Plant and process for the production of synthetic fuels without carbon dioxide emissions

Abstract

a) 一個合成氣體製造裝置，從甲烷、水及二氧化碳製造一種合成粗氣體，其中合成氣體製造裝置包括至少一個反應段及至少一個熱能產生段，其中甲烷、水及二氧化碳在反應段反應產生粗合成氣體，燃料在熱能產生段燃燒產生煙氣，以產生使甲烷及二氧化碳反應產生粗合成氣體所需的熱能；;b) 一個從合成氣體製造裝置產生的粗合成氣體分離出二氧化碳的分離裝置；;c) 一個費托合成裝置，利用費托合成法從在分離裝置內二氧化碳被分離出來的合成氣體產生碳氫化合物；以及;d) 一個提煉裝置，將費托合成裝置產生的碳氫化合物提煉成合成燃料；;此外，此設備還包括e;1)一個將二氧化碳從合成氣體製造裝置經由煙氣排放管排出的煙氣分離出來的分離裝置，及 / 或e;2)一個與合成氣體製造裝置的熱能產生段連接的煙氣回流管，其中i)從煙氣分離出來的二氧化碳直接輸入合成氣體製造裝置，或是先輸入一個二氧化碳壓縮裝置，然後再從該處輸入合成氣體製造裝置，其中ii)此設備還具有一個電解裝置，其作用是將水電解成氫及氧，其中電解裝置具有一個進水管、一個氧氣排放管、以及一個氫氣排放管，其中一個管子從氧氣排放管匯入含氧氣體通往合成氣體製造裝置的輸入管。;

Description

Technical Field

[0001] This invention relates to an apparatus and method for manufacturing synthetic fuels, particularly an apparatus and method for manufacturing aviation turbine fuel, diesel fuel, and / or crude gasoline. Prior Technology

[0002] Currently, a range of different methods exist for manufacturing fuels, such as aviation turbine fuel, diesel, crude gasoline, or other similar fuels. These methods are primarily based on the processing of fossil fuels, such as refining petroleum, liquefying coal, or synthesizing natural gas, water, and oxygen. The synthesis of natural gas, water, and oxygen is also known as "natural gas liquefaction." This method first produces a syngas containing hydrogen and carbon monoxide from natural gas, water, and oxygen, which is then converted into hydrocarbons, primarily long-chain n-alkanes, through Fischer-Tropsch synthesis. These hydrocarbons are then further converted into fuels through cracking and isomerization reactions.

[0003] A similar method is "power liquefaction," which converts electrical energy into synthetic fuels. This method first converts water and carbon dioxide into syngas, and then further processes it into synthetic fuels using a method similar to "natural gas liquefaction."

[0004] An alternative approach known as "power and biomass liquefaction" utilizes biomass (such as biomethane and biogas) or synthetic methane as a carbon source, supplemented by carbon dioxide from the air or point sources, to replace whole fossil carbon sources such as oil or natural gas. For example, this type of method converts methane, water (steam), and carbon dioxide into syngas, which is then further processed into synthetic fuels using methods similar to those mentioned above.

[0005] A major drawback of the methods described above is the generation and emission of large amounts of carbon dioxide. From an environmental policy and climate protection perspective, this is extremely detrimental. Furthermore, these methods require large quantities of fresh water and generate significant amounts of waste gas. However, water of the required purity is a very expensive raw material, and for environmental policy reasons, the large-scale discharge of wastewater is a significant problem. Summary of the Invention

[0006] The purpose of this invention is to provide an apparatus and method for manufacturing synthetic fuels. This apparatus and method should have low energy requirements, produce no carbon dioxide emissions, or at least emit very little carbon dioxide, require only a small amount of fresh water input, and have very small wastewater discharge. Moreover, it can operate using almost only electricity and biomass.

[0007] The above-mentioned objective can be achieved using the equipment described in claim 1. This equipment is for manufacturing synthetic fuels, particularly aviation turbine fuel, diesel fuel, and / or crude gasoline. This equipment includes: a) A (first) syngas manufacturing apparatus for producing a crude syngas containing carbon monoxide, hydrogen, and carbon dioxide from methane, water, and carbon dioxide, wherein the syngas manufacturing apparatus includes at least one reaction section and at least one heat generation section, wherein methane, water, and carbon dioxide react in the reaction section to produce crude syngas, and fuel is burned in the heat generation section to produce flue gas to generate the heat energy required for the reaction of methane and carbon dioxide to produce crude syngas, wherein the reaction section has a methane inlet pipe, a water inlet pipe, at least one carbon dioxide inlet pipe, and a crude syngas outlet pipe, and the heat generation section has a fuel inlet pipe, an oxygen-containing gas inlet pipe, and a flue gas outlet pipe; b) A separation device for separating carbon dioxide from crude syngas produced by a syngas manufacturing unit, comprising a carbon dioxide discharge pipe and a syngas discharge pipe; c) A Fischer-Tropsch synthesis apparatus that uses the Fischer-Tropsch synthesis method to produce hydrocarbons from a synthesis gas from which carbon dioxide is separated in a separation unit; and d) A refining unit that refines hydrocarbons produced by the Fischer-Tropsch synthesis unit into synthetic fuels; In addition, this device also includes: e1) A separation device for separating carbon dioxide from flue gas discharged from a syngas manufacturing apparatus via a flue gas discharge pipe, wherein the separation device has a carbon dioxide discharge pipe, wherein the carbon dioxide discharge pipe of the separation device for separating carbon dioxide from the flue gas discharged from the syngas manufacturing apparatus via the flue gas discharge pipe and the carbon dioxide discharge pipe of the separation device for separating carbon dioxide from the crude syngas produced by the syngas manufacturing apparatus are directly connected to one of at least one carbon dioxide input pipes of the syngas manufacturing apparatus; or the carbon dioxide discharge pipe of the separation device for separating carbon dioxide from the flue gas discharged from the syngas manufacturing apparatus via the flue gas discharge pipe and the carbon dioxide discharge pipe of the separation device for separating carbon dioxide from the crude syngas produced by the syngas manufacturing apparatus are connected to a carbon dioxide compression device, wherein the carbon dioxide compression device has an discharge pipe connected to one of at least one carbon dioxide input pipes of the syngas manufacturing apparatus; and / or e2) A flue gas return pipe connected to a flue gas discharge pipe of a syngas manufacturing apparatus, wherein the flue gas return pipe and a carbon dioxide discharge pipe of a separation device for separating carbon dioxide from the crude syngas produced by the syngas manufacturing apparatus are directly connected to one of at least one carbon dioxide input pipes of the syngas manufacturing apparatus; or the flue gas return pipe and the carbon dioxide discharge pipe of the separation device for separating carbon dioxide from the crude syngas produced by the syngas manufacturing apparatus are connected to a carbon dioxide compression device, wherein the carbon dioxide compression device has an discharge pipe connected to one of at least one carbon dioxide input pipes of the syngas manufacturing apparatus. In addition, this equipment also has an electrolysis unit, which electrolyzes water into hydrogen and oxygen. The electrolysis unit has a water inlet pipe, an oxygen outlet pipe, and a hydrogen outlet pipe. One of the pipes connects to the oxygen outlet pipe and enters the input pipe of the oxygen-containing gas leading to the synthesis gas manufacturing unit.

[0008] The apparatus and method of this invention not only separate carbon dioxide from the reaction products (i.e., crude syngas) remaining in the syngas production apparatus and return it to the syngas production apparatus, but also return all the flue gas generated by the syngas production apparatus to the syngas production apparatus, and / or separate carbon dioxide from the flue gas and then return the separated carbon dioxide to the syngas production apparatus to provide the necessary heat energy for the intense endothermic reaction through combustion. Since all the carbon dioxide generated in the process is fully utilized, carbon dioxide emissions can be reliably avoided. Furthermore, according to this invention, at least a portion of the oxygen-containing gas required for fuel combustion in the heat generation section of the syngas production apparatus is provided by oxygen generated by the electrolysis unit. Therefore, the proportion of air in the combustion gas can be significantly reduced, or even reduced to 0, meaning it is entirely supplied by oxygen generated from the electrolysis of water using electrical energy. By reducing the amount of air in the mixture of fuel, oxygen, and air, the volume of gas that needs to be heated to the combustion temperature in the heat generation section of the syngas production apparatus can be significantly reduced, because the nitrogen (approximately 79% of the air) contained in the air replaced by the oxygen generated by electrolysis has been removed. Because the reaction enthalpy is the same, but the required heating power is significantly reduced, the fuel demand can be greatly reduced, thus reducing the energy requirements of the equipment. Furthermore, this also reduces the volume of carbon dioxide-containing flue gas produced by combustion. This not only reduces the amount of carbon dioxide that must be circulated through the flue gas, thus significantly reducing the cooling power required for the flue gas, but also increases the hydrogen-to-carbon monoxide ratio in the crude synthesis gas. This reduces the amount of hydrogen required to adjust the hydrogen-to-carbon monoxide ratio in the crude synthesis gas to the desired value, wherein the hydrogen input to the synthesis gas production unit is preferably generated within the electrolysis unit. Therefore, according to the present invention, a large portion of the oxygen-containing gas required for fuel combustion in the heat generation section of the synthesis gas production unit, and the hydrogen required to adjust the hydrogen-to-carbon monoxide ratio in the crude synthesis gas to the desired value, is entirely generated by electrolyzing water using electrical energy. Therefore, in principle, all the oxygen-containing gas required for combustion of fuel in the heat generation section of a syngas production apparatus can be provided solely by the electrolysis unit. However, based on safety considerations for syngas production apparatuses, large-scale equipment must be able to input a certain proportion of air or other suitable gases, such as carbon dioxide, to prevent the oxygen content and combustion temperature of the combustion mixture from becoming excessively high. Another particular advantage of the apparatus and method of the present invention is that the wastewater generated by the apparatus in carrying out the method of the present invention, after treatment, can be used as water for electrolysis. A particularly advantageous embodiment of the invention described later herein provides further explanation of this part, thus saving all or most of the fresh water.Even without considering this, the equipment and method of the present invention can significantly reduce the amount of waste gas and wastewater, because the generated waste gas and wastewater can be recycled, for example, for use in an electrolysis unit. The methane used is biomethane or synthetic methane produced from green materials, and the electricity used comes from green electricity. Biomethane can also be replaced by methane from any other source, such as any methane-containing gas mixture, such as biogas, preferably composed of 30 to 70% (volume percentage) methane and 70 to 30% (volume percentage) carbon dioxide, or more preferably 40 to 60% (volume percentage) methane and 60 to 40% (volume percentage) carbon dioxide, for example 50% (volume percentage) methane and 50% (volume percentage) carbon dioxide. Because no natural or fossil raw materials, such as petroleum, natural gas, or other similar raw materials, are used, the method of the present invention is very resource-efficient. Overall, this invention utilizes a fully integrated manufacturing unit to completely convert methane, carbon dioxide generated during the process, and water produced by electricity into synthetic fuels, such as aviation turbine fuel, diesel, and / or crude gasoline, such as kerosene (SAF - "Sustainable Aviation Fuel"), crude gasoline, and / or light gasoline, while avoiding any carbon dioxide emissions, producing no significant persistent exhaust emissions, and significantly reducing wastewater volume. Finally, the method of this invention is characterized by relatively low energy requirements. This advantage stems from the synergistic effect of the electrolysis unit and flue gas treatment, depending on equipment feature e1) or e2).

[0009] According to the present invention, separation device b) separates carbon dioxide from crude synthesis gas produced by the synthesis gas manufacturing unit, Fischer-Tropsch synthesis unit c) uses Fischer-Tropsch synthesis to produce hydrocarbons from the synthesis gas from which carbon dioxide is separated in separation device b), and refining device d) refines the hydrocarbons produced by Fischer-Tropsch synthesis unit c) into synthetic fuels. That is, separation device b) which separates carbon dioxide is connected to synthesis gas manufacturing unit a) via a crude synthesis gas discharge pipe, Fischer-Tropsch synthesis unit c) which uses Fischer-Tropsch synthesis to produce hydrocarbons is connected to separation device b) via a synthesis gas input pipe, and refining device d) is connected to Fischer-Tropsch synthesis unit c) via a hydrocarbon input pipe.

[0010] As mentioned above, the synergistic effect of equipment feature e1) or e2) with the flue gas treatment of the electrolysis unit is the core of this invention. Therefore, it is crucial that during the operation of the equipment of this invention, or during the execution of the method of this invention, all generated carbon dioxide must be separated and returned to the syngas production unit. That is, not only must the carbon dioxide remaining in the reaction products (i.e., crude syngas) of the syngas production unit be separated, but more importantly, all the flue gas generated within the syngas production unit must be returned to the syngas production unit, and / or the carbon dioxide in the flue gas must be separated and returned to the syngas production unit to provide the necessary heat energy for the intense endothermic reaction through combustion. Therefore, according to this invention, the equipment has no carbon dioxide emission pipe, or in other words, the equipment does not emit carbon dioxide during operation. Furthermore, another advantage of the method of this invention is that a completely neutral carbon dioxide balance can be achieved.

[0011] An important component of the equipment of the present invention is a syngas production apparatus (b) for producing a crude syngas containing carbon monoxide, hydrogen, and carbon dioxide from methane, water, and carbon dioxide. The term "producing a crude syngas containing carbon monoxide, hydrogen, and carbon dioxide from methane, water, and carbon dioxide" refers to an initial mixture containing methane, water, and carbon dioxide, but may also contain other components. In particular, biogas can be used as a source of methane, preferably composed of 30 to 70% (volume percentage) methane and 70 to 30% (volume percentage) carbon dioxide, or more preferably 40 to 60% (volume percentage) methane and 60 to 40% (volume percentage) carbon dioxide, for example, 50% (volume percentage) methane and 50% (volume percentage) carbon dioxide. The term "methane inlet pipe" refers to a pipe for feeding a gas containing methane (e.g., biogas) or pure methane. The syngas production apparatus (b) is preferably a dry reformer. The dry reformer preferably contains a nickel oxide catalyst and can operate at pressures of 10 to 50 bar and temperatures of 700 to 1200°C. Besides processing methane and water vapor, the dry reformer can also process carbon dioxide, where these reactions are strongly endothermic. Therefore, the dry reformer requires corresponding heating to provide the energy or heat required for the endothermic reactions. This invention generates the required heat by burning fuel with oxygen-containing gas, which is derived from oxygen produced by electrolysis, or, if necessary, air or other suitable gases. According to a particularly advantageous embodiment of the invention, all or at least almost all of the required fuel comes from the exhaust gases or combustion gases generated during equipment operation, as well as the resulting synthetic fuels; that is, no external fuel supply is required. For example, hydrogen can be used beforehand in a hydrogenation unit to release the methane to be fed into the dry reformer from sulfur contamination.

[0012] Therefore, one proposed improvement of the present invention is that the Fischer-Tropsch synthesis apparatus or refining apparatus has a gas exhaust pipe, or preferably the Fischer-Tropsch synthesis apparatus and the refining apparatus each have a gas exhaust pipe, wherein the gas exhaust pipe or the gas exhaust pipes are connected to a fuel input pipe so as to utilize the calorific value-containing waste gas generated in the Fischer-Tropsch synthesis reaction and refining process as fuel or combustion gas for heating the synthesis gas manufacturing apparatus.

[0013] Furthermore, according to an advantageous embodiment, the refining unit has one or more synthetic fuel product discharge pipes, wherein at least one of these discharge pipes is connected to the fuel input pipe of the syngas production unit via a return pipe. This allows a portion of the synthetic fuel (particularly light gasoline) produced by the refining unit to be returned to the heat generation section of the syngas production unit for use as fuel. If the calorific value of the exhaust gases from the Fischer-Tropsch synthesis unit and the refining unit is insufficient to generate enough heat for the syngas production unit to operate, an appropriate amount of synthetic fuel (particularly light gasoline) produced by the equipment can be input to make up the difference in required energy or heat, thus eliminating the need for additional external fuel input.

[0014] For example, the refining unit may have a kerosene (SAF) product discharge pipe, a crude gasoline product discharge pipe, and a light gasoline product discharge pipe, wherein the return pipes of one or more of these product discharge pipes (preferably the return pipe of the light gasoline product discharge pipe) converge into the fuel input pipe of the synthesis gas manufacturing unit.

[0015] According to another advantageous embodiment of the invention, the apparatus has a control device that controls the amount of synthetic fuel entering the heat generation section of the syngas production apparatus as fuel, so that the syngas production apparatus, or preferably the entire apparatus, does not require external fuel input.

[0016] One proposed improvement of this invention is that the syngas production apparatus, preferably composed of a dry reformer, has one or more tube-buffered reactors, wherein the tubes of each reactor constitute a reaction section, and the area outside the tubes constitutes a heat generation section. This allows for the rapid, uniform, and efficient heating of reactants such as methane, water vapor, and carbon dioxide to the temperatures required for the production of crude synthetic fuels, with a simple structure. One or more suitable nickel oxide catalysts, such as SYNSPIRE™ G1-110 (BASF-catalyst), are placed inside the tubes. When the apparatus is operating, the fuel in the heat generation section of the dry reformer is burned at a pressure of 10 to 50 bar, preferably 20 to 40 bar, for example, 30 bar, heating the reactants inside the tubes of the dry reformer to 700 to 1200°C, preferably 800 to 1100°C, or most preferably 900 to 950°C, for example, 930°C. In practice, even under ideal conditions, the replacement rate of carbon dioxide with methane and water vapor in a dry reformer can only reach a maximum of 50%, resulting in a carbon dioxide concentration of approximately 30% (by volume) in the crude synthetic fuel. This relatively high carbon dioxide concentration places a significant load on Fischer-Tropsch synthesis, which uses carbon dioxide as an inert gas. Furthermore, after Fischer-Tropsch synthesis, carbon dioxide becomes a component of the exhaust gas and is sent back to the dry reformer along with the exhaust gas from the Fischer-Tropsch synthesis unit, mixing with the flue gas and thus reducing the combustion efficiency of the dry reformer. To avoid these drawbacks, in the apparatus of this invention, carbon dioxide is separated from the crude synthesis gas in separation unit b).

[0017] Both the heterohydrocracking reactor and the hydrogen stripper located within the refining unit require hydrogen. Therefore, an improvement proposed in this invention is to use hydrogen produced by an electrolysis unit. Preferably, there is a pipe from the hydrogen exhaust pipe of the electrolysis unit leading to the Fischer-Tropsch synthesis unit and / or a pipe leading to the refining unit. More preferably, there is a pipe from the hydrogen exhaust pipe of the electrolysis unit leading to the Fischer-Tropsch synthesis unit and a pipe leading to the refining unit, and even more preferably, a pipe leading to the syngas production unit.

[0018] The electrolysis apparatus preferably has one or more solid oxide electrolysis chambers, one or more polymer electrolyte membrane electrolysis chambers, and / or one or more alkaline electrolysis chambers. For example, hydrogen is produced using an alkaline-low-temperature-high-pressure-water electrolysis method.

[0019] According to the present invention, the syngas production apparatus has a hydrogen input pipe connected to the gas discharge pipe of the electrolysis unit. Therefore, during operation of the apparatus of the present invention, hydrogen can be input into the syngas production apparatus to adjust the H2 / CO-Mohr ratio of the crude syngas produced by the syngas production apparatus. For this reason, the apparatus preferably has a control device to control the amount of hydrogen input into the syngas production apparatus, so that the H2 / CO-Mohr ratio of the crude syngas produced by the syngas production apparatus is 1.13 to 1.80, preferably 1.15 to 1.50, for example 1.17, 1.39, or 1.43. Dry reformers typically operate at an H2 / CO-Mohr ratio of approximately 1.13. However, a higher H2 / CO-Mohr ratio reduces the carbon dioxide requirement of the dry reformer. According to the present invention, in order to balance the amount of carbon dioxide separated from the flue gas and crude syngas with the carbon dioxide requirement, it is preferable to adjust the H2 / CO-Mohr ratio according to the amount of carbon dioxide separated.

[0020] According to a particularly advantageous embodiment of the invention, the equipment includes a complete water desalination unit, which removes salts and gases from fresh water to achieve the purity requirements for water electrolysis. Therefore, the complete water desalination unit preferably has a fresh water inlet pipe and / or a wastewater inlet pipe for the wastewater generated by the equipment, and preferably removes hydrocarbons from the wastewater first, and has a fully desalinated water outlet pipe connected to the inlet pipe of the electrolysis unit. A particularly advantageous method is to input all fresh water or all or at least almost all process water (preferably pre-purified) generated by the equipment into the complete water desalination unit. Here, all or at least almost all process water means 50% (by weight) or more, 80% (by weight) or more, 90% (by weight) or more, or preferably all of the process water. Excellent results can be achieved if the desalination device can desalinate and degas the input freshwater to a conductivity of less than 20 µS / cm, less than 10 µS / cm, less than 5 µS / cm, or at most no more than 2 µS / cm. To achieve this, a complete water desalination device preferably has one or more cation and anion exchangers, and a membrane device for degassing. Degassing separates carbon dioxide and oxygen from the water. Preferably, the cation and anion exchangers are reduced using sodium hydroxide solution or hydrochloric acid. The resulting wastewater has an ion concentration approximately six times that of water before entering the desalination device, and due to the simultaneous reduction of the cation and anion exchangers, it can be discharged as neutral water into community wastewater treatment facilities.

[0021] According to an improved embodiment of the present invention, the equipment includes a water purification device, the function of which is to purify the process water in the equipment to a level suitable for recycling. Therefore, the amount of fresh water required by the equipment can be minimized. According to this embodiment, the equipment preferably has an inlet pipe from the refining unit to the water purification device and / or an inlet pipe from the Fischer-Tropsch synthesis unit to the water purification device, and / or an inlet pipe from the syngas production unit to the water purification device, and / or an inlet pipe from the carbon dioxide compression unit to the water purification device, to purify the process water in each unit. According to this embodiment, the equipment preferably has an inlet pipe from the refining unit to the water purification device, an inlet pipe from the Fischer-Tropsch synthesis unit to the water purification device, and an inlet pipe from the syngas production unit to the water purification device, and more preferably, also has an inlet pipe from the carbon dioxide compression unit to the water purification device, to purify the process water in each unit.

[0022] For example, a water purification device may have one or more steam stripping units, which function to separate at least 95% of hydrocarbons through steam stripping.

[0023] According to a particularly advantageous embodiment of the invention, the water purification apparatus includes an anaerobic reactor. The water to be purified comes into contact with anaerobic microorganisms within the anaerobic water purification reactor, whereby the microorganisms decompose organic pollutants in the water (primarily into carbon dioxide and methane). Unlike aerobic water purification, anaerobic water purification does not require the expend significant energy to introduce oxygen into the bioreactor. Depending on the type and shape of the biomass used, the reactors for anaerobic water purification can be classified as contact sludge reactors, UASB reactors, EGSB reactors, fixed-bed reactors, and fluidized-bed reactors. In a fixed-bed reactor, microorganisms are attached to a fixed carrier material; in a fluidized-bed reactor, microorganisms are attached to a small, freely movable carrier material; and in UASB and EGSB reactors, microorganisms are added in the form of so-called granular material. A particular advantage of using an anaerobic reactor as the apparatus of this invention is that process water from Fischer-Tropsch synthesis contains a wide variety of hydrocarbons that cannot be removed by other water purification methods (e.g., steam stripping), such as ethanol, aldehydes, carbonic acid, and other similar hydrocarbons. Therefore, the water purification process performed in the anaerobic reactor can be used for water purification in the equipment of this invention. If necessary, desalination can be performed first in a complete water desalination unit, that is, for example, in an electrolysis unit. Furthermore, the water purified and desalinated / degassed in this way can be used as boiler storage water. This can significantly reduce the demand for fresh water, or even eliminate the need for fresh water input altogether. Finally, the biogas produced by the anaerobic reactor of the water purification unit, whose main components are carbon dioxide and methane, can be transported from the water purification unit to the heat generation section of the syngas production unit for use as fuel via a gas return pipe.

[0024] Ideally, the water purification device is connected to the complete desalination unit via a pipe, allowing the purified water to be delivered to the desalination unit. This provides flexibility in meeting the water requirements for desalination and deaeration, particularly the water demand of the electrolysis unit.

[0025] According to another advantageous embodiment of the invention, the water purification device is directly or indirectly connected to the inlet pipe of the syngas manufacturing apparatus so as to input the purified process water into the syngas manufacturing apparatus for reaction.

[0026] According to this embodiment of the invention, it is preferable to provide a vaporization device after the water purification device, wherein the vaporization device is connected to the water inlet pipe of the water purification device and the synthesis gas production device via a pipe, so as to transport water to the synthesis gas production device in the form of water vapor.

[0027] Furthermore, an advantageous approach is to include a control device in the equipment that regulates the flow rate of water purified by the water purification device into the reaction section of the syngas production unit, thereby eliminating the need to input fresh water into the syngas production unit. This helps reduce the amount of fresh water required for the operation of the equipment of the present invention.

[0028] According to an improved embodiment of the invention, the apparatus further comprises a methane steam reformer as a second syngas production unit, which produces a crude syngas containing hydrogen and carbon monoxide from methane, water, and hydrogen. Preferably, the methane steam reformer is connected in parallel with the (first) syngas production unit (preferably a dry reformer), wherein the crude syngas produced by the two syngas production units are first mixed together, and then the crude syngas mixture is fed into a separation unit to separate carbon dioxide. An advantage of this embodiment is that the H2 / CO-Mohr ratio of the crude syngas produced by the methane steam reformer is higher than that of the dry reformer. Because the H2 / CO-Mohr ratio of the crude synthesis gas mixture formed by mixing the crude synthesis gas produced by the dry reformer and the crude synthesis gas produced by the methane steam reformer is higher than that of the crude synthesis gas produced by the dry reformer, this embodiment with one dry reformer and one methane steam reformer, compared to an embodiment with only one dry reformer, does not require or only requires a small amount of hydrogen from the electrolysis unit to adjust the H2 / CO-Mohr ratio of the crude synthesis gas input to the separation unit to the desired value. The methane steam reformer preferably has a hydrogen input pipe, a methane input pipe, a water (steam) inlet pipe, a crude synthesis gas outlet pipe, and a drain pipe. The hydrogen input pipe is connected to the hydrogen outlet pipe of the electrolysis unit, the crude synthesis gas outlet pipe is connected to the crude synthesis gas outlet pipe of the (first) synthesis gas production unit, and the drain pipe is preferably connected to a water purification unit. Preferably, the entire methane steam reformer is heated by current induction; that is, since the methane steam reformer is heated by induction, no carbon dioxide is emitted. The methane steam reformer is preferably operated at low to medium pressures of 1 to 20 bar (e.g., 10 to 15 bar) and reaction temperatures not exceeding 1500°C (e.g., 1000 to 1200°C) to achieve a high syngas (H2 / CO) yield with the lowest possible carbon dioxide content. All carbon dioxide generated by the heated dry reformer and the methane steam reformer is recycled back to the dry reformer; therefore, the equipment of this invention can operate with completely zero carbon dioxide emissions. To accommodate this carbon dioxide and to achieve an ideal H2 / CO-Mohr ratio of approximately 2 before Fischer-Tropsch synthesis, it is preferable to adjust the methane usage in the dry reformer and methane steam reformer to 30-60% to 40-65%, and to adjust the H2 / CO-Mohr ratio of the crude synthesis gas produced by the dry reformer to 1.13-1.80, preferably 1.15-1.20, for example 1.17, and to adjust the H2 / CO-Mohr ratio of the crude synthesis gas produced by the methane steam reformer to 3.20-3.60, for example 3.43.Preferably, the ratio between the dry reformer and the methane steam reformer is adjusted by the amount of methane input to the methane steam reformer, wherein the H2 / CO-moll ratio of the crude synthesis gas produced by the dry reformer is adjusted by the amount of carbon dioxide input, and the H2 / CO-moll ratio of the crude synthesis gas produced by the methane steam reformer is adjusted by the amount of steam input.

[0029] According to an improved embodiment of the invention, in order to separate carbon dioxide from crude synthesis gas, the corresponding separation device b) includes an amine scrubber, which separates carbon dioxide from crude synthesis gas by absorption. The amine scrubber uses at least one absorbent to separate carbon dioxide from crude synthesis gas by absorption, and then returns it directly or indirectly (e.g., via a desorber and a compressor) to the synthesis gas manufacturing apparatus, preferably using an absorbent composed of an amine compound (e.g., monoethanolamine and / or diethylene glycolamine) and water.

[0030] To achieve optimal results, a compressor can be installed downstream of the separator (b). This compressor compresses the syngas to the pressure required for Fischer-Tropsch synthesis. The compressor is connected to the separator via a pipe and to the Fischer-Tropsch synthesis unit via a syngas inlet pipe. The syngas remaining in the compressor is first compressed to the pressure required for Fischer-Tropsch synthesis before being fed into the Fischer-Tropsch synthesis unit. Preferably, the syngas fed into the Fischer-Tropsch synthesis unit contains 80 to 90% (by mass) carbon dioxide and 10 to 15% (by mass) hydrogen.

[0031] Preferably, hydrogen is introduced into the compression unit to adjust the H2 / CO-Mohr ratio of the synthesis gas entering the Fischer-Tropsch synthesis unit to an ideal value. To achieve this, the compression unit preferably has a hydrogen inlet pipe connected to the electrolysis unit. For example, the synthesis gas is adjusted within the compression unit to 30 to 60 bar, or preferably 40 to 50 bar, such as 45 bar, and to 100 to 140 °C, or preferably 110 to 130 °C, such as 120 °C. After the compression unit, the synthesis gas is preferably purified by a three-stage adsorption process to remove halogen compounds, oxygen compounds, and sulfur compounds, which act as catalyst poisons in the Fischer-Tropsch synthesis process, in the ppb range. This purification process is divided into three interconnected stages, each carried out in a corresponding fixed-bed reactor to continuously remove halogen compounds, oxygen compounds, and sulfur compounds. Activated carbon can be added as an additional safety filter. In this purification process, the synthesis gas is first introduced at a pressure of approximately 45 bar and a temperature of approximately 120 °C. An alumina / sodium oxide adsorbent is used as the halogen scavenger. The halogen-removed syngas is then further heated to the operating temperature of the next reactor, 140 to 150°C. This heating is accomplished by a syngas preheater using medium-pressure steam. An alumina / palladium oxide adsorbent is added to the oxygen removal reactor, acting as an oxygen binder. The syngas, still contaminated with trace amounts of sulfur compounds, is then passed through different adsorption layers in the sulfur removal reactor: first, through a layer containing zinc oxide / alumina / sodium oxide adsorbents for the main desulfurization process; then, through a safety layer containing zinc oxide / copper oxide adsorbents for binding with residual sulfur. Activated carbon is added as a filter media to remove other contaminants.

[0032] According to an advantageous method, in order to adjust the synthesis gas input to the Fischer-Tropsch synthesis unit to an ideal H2 / CO-Mohr ratio, the equipment has a control device that controls the amount of hydrogen input to the compressor so that the H2 / CO-Mohr ratio of the synthesis gas discharged from the compressor and input to the Fischer-Tropsch synthesis unit via the synthesis gas input pipe is adjusted to a level greater than 20.

[0033] The syngas is then converted into hydrocarbons in the Fischer-Tropsch synthesis unit. The Fischer-Tropsch synthesis is preferably carried out in a reactor containing a catalyst at a temperature of 170 to 270°C, more preferably 190 to 250°C, or even more preferably 210 to 230°C (e.g., 220°C). Suitable catalysts can be selected from the cobalt catalyst family, such as Co / MMT (montmorillonite) or Co / SiO2. The Fischer-Tropsch synthesis is preferably carried out in one or more tube bundle units, with the catalyst located inside the tubes and the coolant (preferably boiler water) injected into the shell and tube. The Fischer-Tropsch synthesis unit preferably has one or two reactors to enable one-stage or two-stage Fischer-Tropsch synthesis. For cost reasons, one-stage Fischer-Tropsch synthesis is preferred. For example, the Fischer-Tropsch synthesis is carried out at a pressure of 25 to 35 bar, or preferably higher (e.g., 45 bar). The higher the pressure, the smaller the reactor size can be designed. The Fischer-Tropsch synthesis preferably achieves a carbon monoxide replacement rate of 92% or higher. The liquid products (condensate and paraffin) generated during the Fischer-Tropsch synthesis are fed into the downstream refining unit. The intensely exothermic reactions of the Fischer-Tropsch synthesis are cooled using boiler-stored water; specifically, water from the complete desalination unit and / or water purification unit (preferably from the complete desalination unit) is piped into the Fischer-Tropsch synthesis unit and evaporated into steam to cool the reactor. Preferably, at least a significant portion of the steam generated during the Fischer-Tropsch synthesis is fed into the syngas production unit via a steam reflux pipe. Excess steam from the Fischer-Tropsch synthesis unit is preferably used to heat other equipment units, thus eliminating the need for external steam input.

[0034] The products of Fischer-Tropsch synthesis are refined in a refining unit into synthetic fuels, particularly aviation turbine fuel (kerosene), diesel, and / or crude gasoline, such as kerosene (SAF – “Sustainable Aviation Fuel”), crude gasoline, and / or light gasoline. To produce industrial-grade kerosene, diesel, and crude gasoline, the paraffinic products from Fischer-Tropsch synthesis are converted using hydroisomerization and hydrocracking (isohydrocracking) to produce high-value aviation turbine fuels with acceptable cold properties (preferably filterability limiting temperatures equivalent to the “cold filter plugging point” (CFPP), up to -40°C). The heavier products are recycled in the isohydrocracking reactor to produce only kerosene and crude gasoline. The light gases produced in this process flow into the heat generation section of the syngas production unit for use as fuel.

[0035] Therefore, the refining unit is preferably a heterohydrocracking reactor with one or more noble metal catalysts (e.g., platinum or palladium catalysts). Particularly advantageous is that the noble metal catalysts do not require sulfidation, thus avoiding sulfur contamination of the reaction products. This allows the process gases and water vapor generated during heterohydrocracking to be returned to the heat generation section of the syngas production unit. Heterohydrocracking is a catalytic reaction, specifically converting long-chain paraffinic hydrocarbons into shorter-chain isomers with better cooling properties for use in kerosene production. The 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.

[0036] In addition, the refining unit preferably has one or more units for separating light hydrocarbons (i.e., C2H2O). [1] - Hydrogen stripper for C4-hydrocarbons. Finally, the refining unit preferably also has one or more distillation columns for breaking down synthetic fuels into different distillates, such as aviation turbine fuel and diesel, aviation turbine fuel and crude gasoline, aviation turbine fuel, crude gasoline and diesel or similar distillates.

[0037] As mentioned above, it is best to have the hydrogen required for the operation of the heterohydrogenation cracking reactor and hydrogen stripper provided by the electrolysis unit.

[0038] As mentioned above, it is best to purify the process water produced by Fischer-Tropsch synthesis, which contains high concentrations of hydrocarbons (especially ethanol, aldehydes, carbonic acid, and a chemical oxygen demand (CSB) of approximately 40,000 mg / L), by feeding it into a water purification unit so that it can be recycled as process water.

[0039] According to an improved embodiment of the invention, the apparatus further comprises a methanation unit that converts carbon dioxide and hydrogen into methane and water. The methanation unit preferably has a carbon dioxide inlet pipe, a hydrogen inlet pipe preferably connected to a hydrogen outlet pipe of an electrolysis unit, a methane outlet pipe, and a drain pipe, wherein the methane outlet pipe is connected to a methane inlet pipe of a syngas production unit, and the drain pipe of the methanation unit is preferably connected to a water purification unit. The methanation unit may also have a branch pipe that flows into a fuel pipe of the syngas production unit. Since the operation of the apparatus produces carbon dioxide and hydrogen, according to this embodiment, the apparatus itself can produce the methane required by the (first) syngas production unit (preferably a dry reformer) at a very low cost, meaning that methane does not need to be imported from an external source. This is a strongly exothermic reaction, and therefore also produces a large amount of low- and medium-pressure steam that can be used by the apparatus. Since the device of the present invention itself has an electrolysis unit, it can be easily incorporated into a methanation unit. In particular, the water produced by methanation can be purified in a water purification unit and then completely desalinated in a complete water desalination unit to serve as raw material for electrolysis or boiler storage water. The methanation unit is preferably a tube bundle reactor equipped with a nickel catalyst.

[0040] According to a first advantageous embodiment of the invention, the apparatus has a separation device (e1) for separating carbon dioxide from the flue gas discharged from the syngas production unit via a flue gas exhaust pipe. This separation device preferably includes an amine scrubber for separating carbon dioxide from the flue gas, wherein the amine scrubber uses an absorbent, preferably composed of one or more amine compounds, to separate carbon dioxide from the crude syngas. The carbon dioxide separated in this manner from this separation device can be directly fed into the syngas production unit. However, the carbon dioxide separated in this manner from this separation device is preferably fed together with the carbon dioxide separated from the crude syngas by separation device (b) via a corresponding pipe into a carbon dioxide compression device, whereby the carbon dioxide is compressed to a pressure of 25 to 40 bar, or preferably 30 to 35 bar, before being returned to the syngas production unit.

[0041] According to a second advantageous embodiment of the invention, all flue gas produced by the syngas production apparatus is returned to the syngas production apparatus, directly or indirectly. This embodiment is particularly suitable when all or at least most of the oxygen produced by electrolysis is input into the heat generation section of the syngas production apparatus via an oxygen-containing gas input pipe, thus the flue gas contains no inert gases, such as nitrogen, and is treated as if it were air. In this embodiment, the equipment preferably has a flue gas pipe connected to the flue gas exhaust pipe of the syngas production apparatus, wherein the flue gas return pipe (preferably connected to the carbon dioxide exhaust pipe of the separation device b, which separates carbon dioxide from the crude syngas produced by the syngas production apparatus) is directly connected to one of the carbon dioxide input pipes of at least one of the carbon dioxide input pipes of the syngas production apparatus, or both pipes are first connected to a carbon dioxide compression device that compresses the carbon dioxide to the aforementioned ideal pressure, and then the compressed carbon dioxide is returned to the syngas production apparatus.

[0042] A third advantageous embodiment of the invention is a combination of the first two embodiments. In this embodiment, a portion of the flue gas is fed into a carbon dioxide separation device to separate the carbon dioxide from the flue gas. The remaining flue gas, containing unseparated carbon dioxide, is then directly returned to the syngas production apparatus along with the carbon dioxide separated by the two separation devices. Alternatively, it is first fed into a carbon dioxide compression device to compress the mixture to the aforementioned ideal pressure, and then the compressed mixture is returned to the syngas production apparatus. This embodiment is particularly suitable when all or at least most of the oxygen produced by electrolysis is input into the heat generation section of the syngas production apparatus via an oxygen-containing gas input pipe, thus the flue gas contains no inert gases, such as nitrogen, and is treated as if it were air.

[0043] Another object of this patent application is a method for manufacturing synthetic fuels using one of the aforementioned devices, particularly for manufacturing aviation turbine fuel (kerosene), crude gasoline, and / or diesel.

[0044] As mentioned above, the method of the present invention does not emit carbon dioxide, or can be performed without carbon dioxide emissions. For this reason, it is preferable to perform the method in a manner that does not emit carbon dioxide.

[0045] According to an improved version of the present invention, the gas produced by the Fischer-Tropsch synthesis unit, the gas produced by the refining unit, and a portion of the synthetic fuel produced by the refining unit are fed into the heat generation section of the synthesis gas manufacturing unit as fuel. Preferably, the method of the present invention is controlled so that the synthesis gas manufacturing unit, or preferably the entire unit, does not require external fuel input.

[0046] According to the present invention, the apparatus includes an electrolysis unit for electrolyzing water into hydrogen and oxygen. According to the present invention, at least a portion of the oxygen produced by the electrolysis unit is input into the heat generation section of the syngas production apparatus via an oxygen-containing gas input pipe. Furthermore, at least a portion of the hydrogen produced by the electrolysis unit can be fed into the reaction section of the syngas production apparatus to remove sulfur from biomethane and to adjust the H2 / CO-Mohr ratio of the crude syngas produced by the syngas production apparatus. Preferably, the H2 / CO-Mohr ratio of the crude syngas produced by the syngas production apparatus is adjusted to 1.13 to 1.80, more preferably 1.15 to 1.50, for example 1.17, 1.39, or 1.43.

[0047] To obtain good results, a compression device can be installed after the separation unit b). Its function is to compress the gas to the pressure required for Fischer-Tropsch synthesis. A portion of the hydrogen produced by the electrolysis unit is fed into the compression device. The amount of hydrogen fed into the compression device should be controlled so that the H2 / CO-Mohr ratio of the synthesis gas discharged from the compression device and fed into the Fischer-Tropsch synthesis unit is greater than 2.0.

[0048] According to the method of the present invention, a portion of the hydrogen produced by the electrolysis unit is fed into the Fischer-Tropsch synthesis unit so that the H2 / CO-Mohr ratio of the synthesis gas in the Fischer-Tropsch unit is greater than 2.0; a portion of the hydrogen produced by the electrolysis unit is fed into the refining unit; and a portion of the hydrogen produced by the electrolysis unit is fed into the synthesis gas manufacturing unit.

[0049] According to the present invention, in order to minimize the amount of combustion air required to be input into the syngas production apparatus, at least a portion of the oxygen generated by electrolysis is input into the syngas production apparatus. The amount of oxygen supplied by the electrolysis unit to the syngas production apparatus is preferably 1 to 90% (volume percentage), 5 to 60% (volume percentage), 10 to 50% (volume percentage), 20 to 40% (volume percentage), or most preferably 25 to 35% (volume percentage) of the oxygen required by the syngas production apparatus. Any shortfall in the oxygen required by the syngas production apparatus is preferably provided by the air input into the syngas production apparatus. As mentioned above, for large-scale equipment, the oxygen content of the fuel mixture cannot be too high.

[0050] Furthermore, an advantageous approach is to include a water purification unit in which water from the refining unit, the Fischer-Tropsch synthesis unit, and the syngas production unit all flow into the water purification unit, wherein the amount of water purified by the water purification unit is at least sufficient to supply the entire water requirement of the syngas production unit. According to a particularly advantageous approach, water purification includes at least one purification stage carried out in an anaerobic reactor. Biogas, primarily composed of carbon dioxide and methane, generated in the anaerobic reactor of the water purification unit, flows from the water purification unit into the heat generation section of the syngas production unit via a gas return pipe for use as fuel in the heat generation section of the syngas production unit.

[0051] Furthermore, an advantageous approach is that the equipment performing this method includes a water purification device that can desalinate and degas fresh water, bringing the treated water to the purity requirements for water electrolysis. Preferably, the method of the present invention utilizes a desalination device to purify the water to a conductivity of less than 20 µS / cm, less than 10 µS / cm, less than 5 µS / cm, or at most not exceeding 2 µS / cm.

[0052] An improved embodiment of the present invention proposes to perform dry reforming using a nickel oxide catalyst within a syngas production apparatus. Furthermore, an advantageous approach is to perform dry reforming at pressures of 10 to 50 bar and temperatures of 700 to 1200°C.

[0053] According to an advantageous embodiment of the invention, the method further includes methane steam reforming. Methane steam reforming produces a crude synthesis gas containing hydrogen and carbon monoxide from methane, water, and hydrogen, wherein water (steam), methane, and hydrogen from an electrolysis unit are fed into a methane steam reformer, while the crude synthesis gas and water are discharged from the reformer. The crude synthesis gas is fed into a separation unit, and the water is preferably fed into a water purification unit. Methane reforming is preferably carried out at a pressure of 1 to 20 bar, 5 to 15 bar, or more preferably 10 to 15 bar, and a temperature of 800 to 1500°C, 900 to 1300°C, or more preferably 1000 to 1200°C, for example, at a pressure of 12 bar and a temperature of 1100°C. The basic reaction of methane steam reforming is a strongly endothermic reaction, but it cannot completely eliminate the production of carbon dioxide. Methane steam reforming preferably incorporates a nickel catalyst. Prior to steam reforming, the methane should be hydrogenated, ideally using hydrogen from an electrolysis unit to remove sulfur, where the hydrogenated sulfur is separated from the methane. Within the methane steam reformer, the synthesis gas is preferably preheated by the feed and then cooled by the resulting medium-pressure steam. The generated steam and the medium-pressure steam from the dry reformer can all be used as steam for the methane reformer.

[0054] To achieve good results using this method, it is recommended to perform dry reforming within the syngas production unit, and adjust the methane usage in both the dry reformer and the methane steam reformer to 30-60% to 40-65%. Furthermore, an advantageous approach is to adjust the H2 / CO-Mohr ratio of the crude syngas produced by the dry reformer to 1.13-1.80, preferably 1.15-1.20, for example 1.17, and the H2 / CO-Mohr ratio of the crude syngas produced by the methane steam reformer to 3.20-3.60, for example 3.43.

[0055] Furthermore, an advantageous approach is that the methanation in this method converts carbon dioxide and hydrogen from an electrolysis unit into methane and water, wherein the methane is fed into a syngas production unit, and preferably the water into a water purification unit. Preferably, a tube-bundle reactor equipped with a nickel catalyst is used as the methanation unit. Methanation is preferably carried out at a pressure of 10 to 50 bar, or more preferably 30 to 40 bar (e.g., 35 bar) and a temperature of 100 to 500°C, 200 to 400°C, or preferably 250 to 350°C (e.g., 300°C). It is preferable to allow boiler water to flow into the shell of the tube-bundle reactor to cool the intensely exothermic reaction; the low- to medium-pressure steam generated during the cooling process can be used by other parts of the equipment. The carbon dioxide replacement rate within the methanation unit is 80 to 85%, so carbon dioxide remains in the reaction products but can still be fed into the (first) syngas production unit or dry reformer without any problems.

[0056] An improved method of the present invention proposes to discharge the purge gas stream from the Fischer-Tropsch synthesis unit as a combustion gas. This reliably prevents the increase of inert gases (e.g., nitrogen and argon) within the synthesis gas production unit and the Fischer-Tropsch synthesis unit.

[0057] Finally, an advantageous approach is to manufacture aviation turbine fuel, crude gasoline, and / or diesel fuel within a refining unit, with aviation turbine fuel and crude gasoline being the most prominent. For example, kerosene (SAF – "Sustainable Aviation Fuel"), crude gasoline, and light gasoline can be manufactured using the method of this invention. Simple Explanation of the Diagram

[0058] The invention will be further described below with reference to the accompanying drawings, wherein:

[0059] [Figure 1]: A schematic diagram of an embodiment of manufacturing synthetic fuel.

[0060] [Figure 2]: Schematic diagram of another embodiment of manufacturing synthetic fuels.

[0061] [Figure 3]: A schematic diagram of another embodiment of the manufacture of synthetic fuels. Implementation

[0062] The apparatus 10 shown in Figure 1 for manufacturing synthetic fuels includes: a) A synthesis gas manufacturing apparatus 12 for producing a crude synthesis gas containing carbon monoxide, hydrogen, and carbon dioxide from methane, water, and carbon dioxide, wherein the synthesis gas manufacturing apparatus 12 includes at least one reaction section and at least one heat generation section, wherein the methane, water, and carbon dioxide reaction section produces crude synthesis gas, and fuel is burned in the heat generation section to produce flue gas to generate the heat energy required for the reaction of methane and carbon dioxide to produce crude synthesis gas, wherein the reaction section has a methane inlet pipe 14, a steam inlet pipe 16, at least one carbon dioxide inlet pipe 18 leading to the synthesis gas manufacturing apparatus 12, and a crude synthesis gas outlet pipe 20, and the heat generation section has a fuel inlet pipe 22, an oxygen-containing gas inlet pipe 24, and a flue gas outlet pipe 26; b) A separation device 28 for separating carbon dioxide from crude synthesis gas produced by synthesis gas manufacturing unit 12, having a carbon dioxide emission pipe 30 and a synthesis gas emission pipe 32 of the separation device 28; c) A Fischer-Tropsch synthesis unit 34, which uses Fischer-Tropsch synthesis to produce hydrocarbons from the synthesis gas from which carbon dioxide is separated in a separation unit 28; and d) A refining unit 36 ​​refines the hydrocarbons produced by the Fischer-Tropsch synthesis unit 34 into synthetic fuels; In addition, device 10 also includes: e1) A separation device 38 for separating carbon dioxide from the flue gas discharged from the syngas production unit 12 via the flue gas discharge pipe 26, wherein the separation device 38 has a carbon dioxide discharge pipe 40 of the separation device 38, wherein the carbon dioxide discharge pipe 40 of the separation device 38 for separating carbon dioxide from the flue gas discharged from the syngas production unit 12 via the flue gas discharge pipe 26 and the carbon dioxide discharge pipe 30 of the separation device 28 for separating carbon dioxide from the crude syngas produced by the syngas production unit 12 are connected to a carbon dioxide compression device 42, wherein the carbon dioxide compression device has an discharge pipe connected to a carbon dioxide input pipe 18 of the syngas production unit 12.

[0063] The syngas compression unit 43 is located downstream of the separation unit 28 and its function is to compress the syngas to the pressure required for Fischer-Tropsch synthesis. The syngas compression unit 43 is connected to the separation unit 28 via a syngas discharge pipe 32 and to the Fischer-Tropsch synthesis unit 34 via a syngas input pipe 44. The Fischer-Tropsch synthesis unit 34 is connected to the refining unit 36 ​​via a pipe 46, wherein the refining unit 36 ​​has two synthetic fuel product discharge pipes 48', 48''.

[0064] A gas return pipe 50 from the Fischer-Tropsch synthesis unit 34 merges into the fuel input pipe 22 of the synthesis gas production unit 12. A methane input pipe 15 from outside the unit merges into the fuel input pipe 22 of the synthesis gas production unit 12. A gas return pipe 52, an engine fuel return pipe 54, and a biogas return pipe 51 from the refining unit 36 ​​merge into the fuel input pipe 22 of the synthesis gas production unit 12.

[0065] In addition, the equipment 10 also has an electrolysis unit 56, which electrolyzes water into hydrogen and oxygen. The electrolysis unit 56 has a water inlet pipe 58, an oxygen outlet pipe 60, and a hydrogen outlet pipe 62. From the hydrogen outlet pipe 62, there are branches: a pipe 63 leading to the synthesis gas production unit 12, a pipe 64 leading to the Fischer-Tropsch synthesis unit 34, a hydrogen inlet pipe 65 leading to the synthesis gas compression unit 43, and a pipe 66 leading to the refining unit 36. From the oxygen outlet pipe 60, there is an oxygen pipe 68 that merges into the oxygen-containing gas inlet pipe 24 of the synthesis gas production unit 12, and an oxygen product pipe 69 that exits from the equipment 10. A combustion air inlet pipe 25 merges into the oxygen-containing gas inlet pipe 24 of the synthesis gas production unit 12.

[0066] In addition, the device 10 also has a complete water desalination device 70, wherein the complete water desalination device 70 has a fresh water inlet pipe 72 and a complete desalination water outlet pipe 74, wherein the complete desalination water outlet pipe 74 is connected to the water inlet pipe 58 of the electrolysis device 56.

[0067] In addition, the equipment 10 also includes a water purification device 76, which purifies the process water in the equipment to a level suitable for recycling. The water purification device 76 has an anaerobic reactor where the water to be purified comes into contact with anaerobic microorganisms, allowing the microorganisms to decompose organic pollutants in the water (mainly into carbon dioxide and methane). A process water discharge pipe 78 from the Fischer-Tropsch synthesis unit 34, a process water discharge pipe 80 from the refining unit 36, a process water discharge pipe 81 from the carbon dioxide compression unit 42, and a process water discharge pipe 82 from the syngas production unit 12 all lead to the water purification device 76. Furthermore, the equipment 10 also includes an evaporator 84, which is connected to the water purification device 76 via a process water inlet pipe 86. Additionally, the evaporator 84 is connected via a pipe to a steam inlet pipe 16 leading to the syngas production unit 12. Finally, the water purification unit 76 has a process water input pipe 88 leading to the complete desalination unit 70, and a biogas return pipe 51 leading to the heat generation section of the synthesis gas production unit 12. The biogas return pipe 51 is used to return the biogas produced by the anaerobic reactor of the water purification unit 76. The main components of the biogas are carbon dioxide and methane, for example, in a ratio of approximately 1:1.

[0068] The separation unit 38, which discharges flue gas from the equipment 10, has a boiler storage water inlet pipe 27, a nitrogen outlet pipe 41, and a process water outlet pipe 83 for separating carbon dioxide and allowing it to enter the water purification unit 76. Furthermore, the complete water desalination unit 70 also has a boiler condensate inlet pipe 71, a boiler storage water outlet pipe 73, and a wastewater outlet pipe 75 for discharging wastewater from the equipment 10.

[0069] When the equipment 10 is operating, methane is introduced into the reaction section of the syngas production unit 12 via methane inlet pipe 14, water (steam) is introduced into the syngas production unit 12 via water (steam) inlet pipe 16, and carbon dioxide is introduced into the syngas production unit 12 via carbon dioxide inlet pipe 18. These three raw materials react in the reaction section of the syngas production unit 12 to produce crude syngas. The energy or heat required for this intense endothermic reaction is provided by the fuel burned in the heat generation section of the syngas production unit 12. For this purpose, fuel is introduced into the heat generation section of the syngas production unit 12 via fuel inlet pipe 22, and oxygen-containing gas is introduced via oxygen-containing gas inlet pipe 24. The fuel mentioned above comes from the exhaust gas or fuel produced by device 10, specifically the exhaust gas from the Fischer-Tropsch synthesis unit 34 input to the synthesis gas production unit 12 via gas return pipe 50, the exhaust gas from the refining unit 36 ​​input to the synthesis gas production unit 12 via gas return pipe 52, the synthetic fuel (light gasoline) input to the synthesis gas production unit 12 via engine fuel return pipe 54, and the biogas from the water purification unit 76 input to the synthesis gas production unit 12 via biogas return pipe 51. For example, the combustion of fuel in the heat generation section of the synthesis gas production unit 12 is carried out under conditions of 1.5 bar pressure and 1100°C temperature. The crude synthesis gas produced in the reaction section of the synthesis gas production unit 12 is discharged through the crude synthesis gas exhaust pipe 20 and input into the separation unit 28. The flue gas produced by combustion in the heat generation section of the synthesis gas production unit 12 is discharged through the flue gas exhaust pipe 26 and input into the separation unit 38. In the separation unit 28, the carbon dioxide separated from the flue gas is input into the carbon dioxide compression unit 42 through the carbon dioxide exhaust pipe 30 of the separation unit 28. Furthermore, within the separation unit 38, the carbon dioxide separated from the flue gas is input to the carbon dioxide compression unit 42 via the carbon dioxide emission pipe 40 of the separation unit 38. For example, the carbon dioxide is compressed to a pressure of 32.5 bar in the carbon dioxide compression unit 42, and then the compressed carbon dioxide is input to the syngas production unit 12 via the carbon dioxide input pipe 18 leading to the syngas production unit 12. Since this method replaces the carbon dioxide consumed in producing syngas with the carbon dioxide produced by burning fuel, carbon dioxide emissions can be avoided. For this reason, the method of the present invention operates in a carbon-neutral manner. Moreover, the implementation of this method requires no or at least almost no external fuel input.

[0070] The syngas, from which carbon dioxide is separated in the separation unit 28, is fed into the syngas compression unit 43 via the syngas exhaust pipe 32. Simultaneously, hydrogen from the electrolysis unit 56 is fed into the syngas compression unit 43 via the hydrogen input pipe 65. For example, the syngas is compressed to a pressure of 42.5 bar in the compression unit, while the temperature is adjusted to 120°C. Furthermore, after passing through the compression unit, the syngas is then purified with a suitable adsorbent to separate halogens, sulfur, nitrogen, oxygen, metals, and other contaminants. During this process, the amount of hydrogen fed into the syngas compression unit 43 should be controlled to ensure that the H2 / CO-Mohr ratio of the syngas is greater than 2.0. This syngas is then fed into the Fischer-Tropsch synthesis unit 34 via the syngas input pipe 44, where it is converted into hydrocarbons, particularly n-alkane hydrocarbons. These hydrocarbons are fed into the refining unit 36 ​​via pipe 46, where they are hydrogenated and hydrocracking (isohydrocracking) into synthetic crude fuel. They are then separated in a hydrogen stripper and fractionated into light gasoline, crude gasoline, and kerosene (SAF - "Sustainable Aviation Fuel") in one or more distillation columns of the refining unit 36. The crude gasoline and kerosene are discharged from the equipment 10 via pipe 48 (gasoline) and pipe 48' (kerosene). The light gasoline is fed into the synthesis gas production unit 12 via engine fuel return pipe 54 and fuel input pipe 22. Wastewater from the Fischer-Tropsch synthesis unit 34, refining unit 36, carbon dioxide compression unit 42, carbon dioxide separation unit 38, and syngas production unit 12 is fed into a water purification unit 76 via process water discharge pipe 78 of the Fischer-Tropsch synthesis unit 34, process water discharge pipe 80 of the refining unit 36, process water discharge pipe 81 of the carbon dioxide compression unit 42, process water discharge pipe 82 of the syngas production unit 12, and process water discharge pipe 83 of the carbon dioxide separation unit 38. Within the water purification unit, the wastewater is purified by anaerobic microorganisms. A portion of the purified process water is fed into an evaporation unit 84 via process water input pipe 86, where it is completely evaporated. The resulting water vapor is fed into the syngas production unit 12 via water vapor input pipe 16. Another portion of the purified process water is fed into a complete water desalination unit 70 via process water input pipe 88.

[0071] The pure water required by the electrolysis unit 56 is fully desalinated fresh water and purified process water treated by the complete desalination unit 70, and is input into the electrolysis unit 56 through the inlet pipe 58. The hydrogen produced by the electrolysis unit 56 is input into the synthesis gas production unit 12, the Fischer-Tropsch synthesis unit, the synthesis gas compression unit 43, and the refining unit 36 ​​through pipes 62, 63, 64, 65, and 66. A portion of the oxygen produced by the electrolysis unit 56 is mixed with air input through pipe 25 via oxygen pipe 68 to form an oxygen-containing gas, which is then input into the heat generation section of the synthesis gas production unit 12. The remaining portion of the oxygen produced by the electrolysis unit 56 is discharged from the equipment 10 through oxygen product pipe 69.

[0072] The device 10 in Figure 2 is equivalent to the device 10 in Figure 1, the only difference being that the device 10 in Figure 2 also includes a methanation unit 11 that converts hydrogen and carbon dioxide into methane and water. The methanation unit 11 has a carbon dioxide input pipe 19, a hydrogen input pipe 67 connected to the hydrogen discharge pipe 62 of the electrolysis unit 56, a methane discharge pipe 17 of the methanation unit 11, and a process water discharge pipe 87. The methane discharge pipe 17 and the methane input pipe 14 of the methanation unit 11 are connected to the syngas production unit 12, and the process water discharge pipe 87 of the methanation unit 11 is connected to the water purification unit 76. A branch pipe 15 from the methane discharge pipe 17 merges into the fuel input pipe 22 leading to the syngas production unit. Since the device 10 produces carbon dioxide and hydrogen during operation, in this embodiment, the device 10 itself can produce the methane required by the (first) syngas production unit (i.e., the dry reformer) at a very low cost, thus eliminating the need for external methane input. This is a strongly exothermic reaction, and therefore it will also produce a large amount of low-pressure and medium-pressure steam that can be used by the equipment. Since the equipment itself has an electrolysis unit 56, the methanation unit 11 can be incorporated into the equipment 10 without any difficulty. In particular, the water produced by methanation can be purified in the water purification unit 76 and then completely desalinated in the water desalination unit 70, so as to be used as raw material for electrolysis or boiler storage water.

[0073] The apparatus 10 in Figure 3 is equivalent to the apparatus 10 in Figure 1, except that the apparatus 10 in Figure 2 also has a methane steam reformer 31 as a second synthesis gas production unit, which produces crude synthesis gas containing carbon monoxide and hydrogen from methane, water, and hydrogen. Preferably, the methane steam reformer 31 is connected in parallel with the (first) synthesis gas production unit 12 (dry reformer), wherein the crude synthesis gases produced by the two synthesis gas production units 12, 31 are first mixed together, and then the crude synthesis gas mixture is fed into the separation unit 28 to separate carbon dioxide from the crude synthesis gas. The methane steam reformer 31 has a hydrogen input pipe 61, a methane input pipe 13, a water (steam) input pipe 23, a crude synthesis gas discharge pipe 21, and a process water discharge pipe 85. The hydrogen input pipe 61 is connected to the hydrogen discharge pipe 62 of the electrolysis unit 56. The crude synthesis gas discharge pipe 21 is connected to the crude synthesis gas discharge pipe 20 of the crude synthesis gas input pipe 29 leading to the separation unit 28 (first) synthesis gas production unit 12. The process water discharge pipe 85 is connected to the water purification unit 76. The methane steam reformer 31 can be heated entirely by induction heating; that is, since the methane steam reformer 31 is induction heated, it does not emit carbon dioxide. The methane steam reformer 31 operates at low to medium pressures of 1 to 20 bar (e.g., 10 to 15 bar) and reaction temperatures not exceeding 1500°C (e.g., 1000°C to 1200°C). One advantage of this embodiment is that the H2 / CO-Mohr ratio of the crude synthesis gas produced by the methane steam reformer 31 is greater than that of the dry reformer 12. Since the H2 / CO-Mohr ratio of the crude synthesis gas mixture formed by the dry reformer 12 and the methane steam reformer 31 is higher than that of the crude synthesis gas produced by the dry reformer 12, this embodiment with one dry reformer 12 and one methane steam reformer 31 does not require hydrogen from the electrolysis unit 56 to adjust the H2 / CO-Mohr ratio of the crude synthesis gas input to the separation unit 28 to the desired value, compared to an embodiment with only one dry reformer 12. Furthermore, the device 10 also includes a combustion gas exhaust pipe 55.

[0074] The present invention will be described below by way of example, but these examples do not limit the present invention in any way.

[0075] Example 1 [ ] [ ] The process simulation software PRO / II (AVEVA) was used to simulate the production of synthetic fuels using the equipment shown in Figure 1 and described above, with a daily output of 144.456 liters of kerosene (SAF - "Sustainable Aviation Fuel") and 42.528 liters of crude gasoline (crude volatile oil). The product streams measured in each pipe are shown in the table below: [ ] [ ] [total] [gas] [liquid] [serial number] [name] [kg / h] [Nm³ / h] [Std.m³ / h] 14 The input pipe for methane to the synthesis gas production unit 6.150 8.592 15 Methane inlet pipe leading to fuel inlet pipe 385 538 16 Water vapor enters the inlet pipe of the synthesis gas manufacturing unit 11.000 13.686 18 Carbon dioxide input pipe leading to the synthesis gas production unit 21.260 10.839 20 crude syngas emission pipe 29.699 38.172 twenty two fuel inlet pipe 4.398 5.055 twenty four Oxygen gas inlet tube 44.232 34.100 25 Combustion air inlet pipe 40.182 31.263 26 flue gas exhaust pipe 48.630 38.690 27 Boiler storage water inlet pipe 386 0.39 30 Carbon dioxide emission pipe of separation unit 28 11.108 5.632 32 Syngas emission pipe 18.591 32.445 40 Carbon dioxide emission pipe of separation unit 38 10.384 5.388 41 Nitrogen exhaust pipe 38.246 26.716 44 Synthesis gas inlet pipe leading to the Fischer-Tropsch synthesis unit 19.352 40.580 46 Input pipe leading to the refining unit 6.210 8,0 48' crude gasoline (crude volatile) product emission pipe 1.210 1,77 48” Kerosene product discharge pipe 4.550 6.06 50 Gas reflux pipe of Fischer-Tropsch synthesis unit 3.373 4.167 51 biogas return pipe leading to the syngas production unit 206 203 52 Gas reflux pipe of refining unit 88 39 54 Engine fuel return pipe 346 0.55 58 The water inlet pipe of the electrolysis unit 7.499 7,5 60 Oxygen exhaust pipe of electrolysis unit 6.632 4.711 62 Hydrogen emission pipe of electrolysis unit 867 9.203 63 Hydrogen input pipe leading to the synthesis gas production unit 17,7 140 64 Hydrogen input pipe leading to the Fischer-Tropsch synthesis unit 0 0 65 Hydrogen input pipe leading to the carbon dioxide compression unit 761 8.127 66 Hydrogen input pipe leading to the refining unit 88 937 68 oxygen tube 4.050 2.837 69 Oxygen product tube 2.582 1.809 71 Boiler condensate inlet pipe 56.431 56,5 72 Freshwater inlet / outlet pipe 3.494 3,5 73 Boiler storage water discharge pipe 59.490 59,5 74 Fully desalinated water discharge pipe 7.499 7,5 75 Wastewater discharge pipes leaving the equipment 950 0.96 78 Process water discharge pipe of Fischer-Tropsch synthesis unit 9.769 9,8 80 Process water discharge pipe of refining unit 104 0.10 81 Process water discharge pipe of carbon dioxide compression unit 231 0,23 82 Process water discharge pipe of syngas manufacturing unit 8.729 8,74 83 Process water discharge pipe of carbon dioxide separation unit 386 0.39 86 The process water input pipe of the evaporation unit of the water purification device 11.000 11,0 88 The process water inlet pipe of the water purification unit's complete desalination unit 8.014 8,0

[0076] Example 2 [ ] [ ] The process simulation software PRO / II (AVEVA) was used to simulate the production of synthetic fuels using the equipment shown in Figure 2 and described above, with a daily output of 145.827 liters of kerosene (SAF - "Sustainable Aviation Fuel") and 42.883 liters of crude gasoline (crude volatile oil). The product streams measured in each pipe are shown in the table below: [ ] [ ] [total] [gas] [liquid] [serial number] [name] [kg / h] [Nm³ / h] [Std.m³ / h] 14 methane inlet pipe 7.710 10.323 15' Branch pipe that merges into the fuel input pipe 413 552 16 Water vapor enters the inlet pipe of the synthesis gas manufacturing unit 11.000 13.686 17 methane emission pipe of methanation unit 8.122 10.875 18 Carbon dioxide input pipe leading to the synthesis gas production unit 23.200 11.829 19 Carbon dioxide input pipe leading to the methanation unit 18.094 9.284 20 crude syngas emission pipe 31.856 38.994 twenty two fuel inlet pipe 4461 5.110 twenty four Oxygen gas inlet tube 40.460 31.102 25 Combustion air inlet pipe 35.560 27.670 26 flue gas exhaust pipe 44.921 35.734 27 Boiler storage water inlet pipe 386 0.39 30 Carbon dioxide emission pipe of separation unit 28 13.138 6.670 32 Syngas emission pipe 18.718 32.234 40 Carbon dioxide emission pipe of separation unit 38 10.326 5.358 41 Nitrogen exhaust pipe 34.595 23.690 44 Synthesis gas inlet pipe leading to the Fischer-Tropsch synthesis unit 19.539 41.006 46 Input pipe leading to the refining unit 6.270 8,1 48' crude gasoline (crude volatile) product emission pipe 1.222 1,78 48” Kerosene product discharge pipe 4.593 6,12 50 Gas reflux pipe of Fischer-Tropsch synthesis unit 3.406 4.210 51 biogas return pipe leading to the syngas production unit 206 203 52 Gas reflux pipe of refining unit 88 39 54 Engine fuel return pipe 349 0.55 58 The water inlet pipe of the electrolysis unit 35.696 36,8 60 Oxygen exhaust pipe of electrolysis unit 31.570 22.113 62 Hydrogen emission pipe of electrolysis unit 4.127 45.439 63 Hydrogen input pipe leading to the synthesis gas production unit 17,7 140 64 Hydrogen input pipe leading to the Fischer-Tropsch synthesis unit 0 0 65 Hydrogen input pipe leading to the carbon dioxide compression unit 821 8.764 66 Hydrogen input pipe leading to the refining unit 88 937 67 Hydrogen input pipe leading to the methanation unit 3200 35.560 68 Oxygen pipe leading to the synthesis gas manufacturing unit 4.900 3.432 69 Oxygen product tube 26.670 18.681 71 Boiler condensate inlet pipe 106.368 106,6 72 Freshwater inlet / outlet pipe 20.135 20,2 73 Boiler storage water discharge pipe 110.963 111,2 74 Fully desalinated water discharge pipe 35.696 35,8 75 Wastewater discharge pipes leaving the equipment 2500 2,51 78 Process water discharge pipe of Fischer-Tropsch synthesis unit 9.863 9,9 80 Process water discharge pipe of refining unit 105 0.11 81 Process water discharge pipe of carbon dioxide compression unit 264 0,27 82 Process water discharge pipe of syngas manufacturing unit 10.072 10,1 83 Process water discharge pipe of carbon dioxide separation unit 386 0.39 86 The process water input pipe of the evaporation unit of the water purification device 11.000 11,0 87 Process water discharge pipe of methanation unit 13.172 13,2 88 The process water inlet pipe of the water purification unit's complete desalination unit 22.656 22,7

[0077] Example 3 [ ] [ ] The process simulation software PRO / II (AVEVA) was used to simulate the production of synthetic fuel using the equipment shown in Figure 3 and described above, according to the method of this invention. The daily output was 148.096 liters of kerosene (SAF - "Sustainable Aviation Fuel"), 43.130 liters of crude gasoline (crude volatile oil), 13.422 liters of liquid light hydrocarbons, and 20.6 million liters of combustion gases. The product streams measured in each tube are shown in the table below: [ ] [ ] [total] [gas] [liquid] [serial number] [name] [kg / h] [Nm³ / h] [Std.m³ / h] 13 methane inlet pipe leading to the methane steam reformer 4.150 5.798 14 The input pipe for methane to the synthesis gas production unit 3.400 4.750 16 Water vapor enters the inlet pipe of the synthesis gas manufacturing unit 6.109 7.601 18 Carbon dioxide input pipe leading to the synthesis gas production unit 16.090 8.204 20 crude syngas emission pipe 20.079 22.707 twenty one crude synthesis gas exhaust pipe of methane steam reformer 9.277 23.782 twenty two fuel inlet pipe 2.974 3.622 twenty three Water (steam) inlet pipe of methane steam reformer 8.000 9.953 twenty four Oxygen gas inlet tube 33.639 26.108 25 Combustion air inlet pipe 32.772 25.500 26 flue gas exhaust pipe 36.613 29.1137 27 Boiler storage water inlet pipe 342 0,34 29 crude synthesis gas input pipe 29.357 46.489 30 Carbon dioxide emission pipe of separation unit 28 9.669 4.886 32 Syngas emission pipe 19.688 41.481 40 Carbon dioxide emission pipe of separation unit 38 6.645 3.448 41 Nitrogen exhaust pipe 29.968 21.720 44 Synthesis gas inlet pipe leading to the Fischer-Tropsch synthesis unit 19.688 41.481 46 Input pipe leading to the refining unit 6.317 8,2 48 Light hydrocarbon product emission pipe 352 0.56 48' crude gasoline (crude volatile) product emission pipe 1.231 1,8 48” Kerosene product discharge pipe 4.628 6,17 50 Gas reflux pipe of Fischer-Tropsch synthesis unit 3.432 4.240 51 biogas return pipe leading to the syngas production unit 206 203 52 Gas reflux pipe of refining unit 88 39,4 53 Light hydrocarbon gas reflux pipe 2.768 3.419 54 Engine fuel return pipe 664 821 55 Combustion gas exhaust pipe 752 861 58 The water inlet pipe of the electrolysis unit 975 0.98 60 Oxygen exhaust pipe of electrolysis unit 867 608 61 Hydrogen input pipe leading to the methane steam reformer synthesis gas production unit 11,5 91 62 Hydrogen emission pipe of electrolysis unit 108 1097 63 Hydrogen input pipe leading to the synthesis gas production unit 9,8 78 64 Hydrogen input pipe leading to the Fischer-Tropsch synthesis unit 0 0 66 Hydrogen input pipe leading to the refining unit 87 927 68 oxygen tube 867 608 69 Oxygen product tube 0 0 71 Boiler condensate inlet pipe 48.987 49,1 72 Freshwater inlet / outlet pipe 506 0.51 73 Boiler storage water discharge pipe 58.483 58,6 74 Fully desalinated water discharge pipe 975 0.98 75 Wastewater discharge pipes leaving the equipment 1732 1,74 78 Process water discharge pipe of Fischer-Tropsch synthesis unit 9.938 9.96 80 Process water discharge pipe of refining unit 106 0,11 81 Process water discharge pipe of carbon dioxide compression unit 224 0,22 82 Process water discharge pipe of syngas manufacturing unit 5.530 5,54 83 Process water discharge pipe of carbon dioxide separation unit 342 0,34 85 Process water discharge pipe of methane steam reformer 2.885 2,89 86 The process water input pipe of the evaporation unit of the water purification device 6.109 6,12 88 The process water inlet pipe of the water purification unit's complete desalination unit 12.709 12.73

[0078] 10: Equipment for manufacturing synthetic fuels 11: Methanation Unit 12: (First) Syngas Production Unit / Dry Reformer 13: Methane inlet pipe 14: Methane inlet pipe 15: Methane inlet pipe 15': Branch pipe connecting to the fuel input pipe 16: Steam inlet pipe 17: Methane emission pipe 18: Carbon dioxide input pipe 19: Carbon dioxide input pipe 20: Crude Synthetic Gas Emission Pipe 21: Crude Synthetic Gas Emission Pipe 22: Fuel Inlet Pipe 23: Water (steam) inlet pipe of methane steam reformer 24: Oxygen-containing gas inlet tube 25: Combustion air inlet pipe 26: Flue gas emission pipe 27: Boiler storage water inlet pipe 28: Separation device for separating carbon dioxide from crude synthesis gas 29: Crude synthesis gas input pipe 30: Carbon dioxide emission pipe 31: Methane steam reformer (second synthesis gas production unit) 32: Syngas emission pipe 34: Fischer-Tropsch synthesis apparatus 36: Refining equipment 38: Separation device for separating carbon dioxide from flue gas 40: Carbon dioxide emission pipe 41: Nitrogen emission pipe 42: Carbon dioxide compression device 43: Syngas Compression Unit 44: Syngas Inlet Pipe 46: Input pipe leading to the refining unit 48,48',48'': Synthetic fuel product emission pipe 50: Gas reflux pipe of Fischer-Tropsch synthesis unit 51: Biogas return pipe leading to the syngas production unit 52: Gas reflux pipe of refining unit 53: Light hydrocarbon gas reflux pipe 54: Engine fuel return pipe 55: Combustion gas exhaust pipe 56: Electrolysis apparatus 58: Water inlet pipe 60: Oxygen exhaust pipe 61: Hydrogen inlet pipe 62: Hydrogen emission pipe 63: Hydrogen input pipe 64: Hydrogen inlet pipe 65: Hydrogen inlet pipe 66: Hydrogen inlet pipe 67: Hydrogen inlet pipe 68: Oxygen tubing 69: Oxygen Product Pipe 70: Complete water desalination device 71: Boiler condensate inlet pipe 72: Freshwater inlet / outlet pipe 73: Boiler storage water discharge pipe 74: Total Demineralized Water Discharge Pipe 75: Wastewater discharge pipe 76: Water purification device 78: Process water discharge pipe 80: Process water discharge pipe 81: Process water discharge pipe 82: Process water discharge pipe 83: Process water discharge pipe 84: Evaporation apparatus 85: Process water discharge pipe 86: Process water inlet pipe 87: Process water discharge pipe 88: Process water inlet pipe

Claims

1. An apparatus (10) for manufacturing synthetic fuels, comprising: a) A syngas manufacturing apparatus (12) for producing a crude syngas containing carbon monoxide, hydrogen, and carbon dioxide from methane, water, and carbon dioxide, wherein the syngas manufacturing apparatus (12) includes at least one reaction section and at least one heat generation section, wherein the methane, water, and carbon dioxide reaction section produces crude syngas, and fuel is burned in the heat generation section to produce flue gas to generate the heat energy required for the reaction of methane and carbon dioxide to produce crude syngas, wherein the reaction section has a methane inlet pipe (14), a water inlet pipe (16), at least one carbon dioxide inlet pipe (18) leading to the syngas manufacturing apparatus (12), and a crude syngas exhaust pipe (20), and the heat generation section has a fuel inlet pipe (22), an oxygen-containing gas inlet pipe (24), and a flue gas exhaust pipe (26); b) A separation device (28) for separating carbon dioxide from the crude syngas produced by the syngas manufacturing apparatus (12), having a carbon dioxide exhaust pipe (30) and a syngas exhaust pipe (32) of the separation device (28); c) The Fischer-Tropsch synthesis unit (34) uses the synthesis gas from which carbon dioxide is separated in the separation unit (28) to produce hydrocarbons; and d) a refining unit (36) for refining hydrocarbons produced by the Fischer-Tropsch synthesis unit (34) into synthetic fuels; in addition, the equipment (10) also includes: e1) A separation device (38) for separating carbon dioxide from the flue gas discharged from the thermal energy generation section of the syngas production apparatus (12) via a flue gas discharge pipe (26), wherein the separation device (38) has a carbon dioxide discharge pipe (40) of the separation device (38), wherein the carbon dioxide discharge pipe (40) of the separation device (38) and the carbon dioxide discharge pipe (30) of the separation device (28) are directly connected to a carbon dioxide input pipe in at least one carbon dioxide input pipe (18) of the syngas production apparatus (12), or the carbon dioxide discharge pipe (40) of the separation device (38) and the carbon dioxide discharge pipe (30) of the separation device (28) are connected to a carbon dioxide compression device (42), wherein the carbon dioxide compression device (42) has an discharge pipe connected to at least one carbon dioxide input pipe (18) of the syngas production apparatus (12); and / or e2) A flue gas return pipe is connected to the flue gas discharge pipe (26) of the syngas manufacturing apparatus (12), wherein the flue gas return pipe and the carbon dioxide discharge pipe (30) of the separation device (28) are directly connected to at least one carbon dioxide input pipe (18) of the syngas manufacturing apparatus (12), or the flue gas return pipe and the carbon dioxide discharge pipe (30) of the separation device (28) are connected to a carbon dioxide compression device (42), wherein the carbon dioxide compression device (42) has an discharge pipe connected to at least one carbon dioxide input pipe (18) of the syngas manufacturing apparatus (12); In addition, the device (10) also has an electrolysis unit (56) which electrolyzes water into hydrogen and oxygen. The electrolysis unit (56) has a water inlet pipe (58), an oxygen outlet pipe (60), and a hydrogen outlet pipe (62). The oxygen pipe (68) flows from the oxygen outlet pipe (60) into the oxygen-containing gas inlet pipe (24) of the synthesis gas manufacturing device (12).

2. The apparatus (10) of claim 1, wherein the synthesis gas manufacturing apparatus (12) further comprises a hydrogen input pipe (63) leading from the hydrogen discharge pipe (62) of the electrolysis unit to the synthesis gas manufacturing apparatus (12).

3. The apparatus (10) of claim 1 or 2, wherein the synthesis gas production apparatus (12) is a dry reformer containing a nickel oxide catalyst and capable of operating at pressures of 10 to 50 bar and temperatures of 700 to 1200°C.

4. The apparatus (10) of claim 1 or 2, wherein the Fischer-Tropsch synthesis apparatus (34) and / or the refining apparatus (36) have gas discharge pipes (50, 52) connected to the fuel input pipe (22) of the synthesis gas production apparatus (12).

5. The apparatus (10) of claim 1 or 2, wherein the refining unit (36) has one or more synthetic fuel product discharge pipes (48, 48', 48''), wherein at least one of the one or more synthetic fuel product discharge pipes (48, 48', 48'') is connected via a return pipe (54) to the fuel input pipe (22) of the synthetic gas manufacturing unit (12), such that a portion of the synthetic fuel produced by the refining unit (36) can be returned to the heat generation section of the synthetic gas manufacturing unit (12) for use as fuel.

6. The device (10) of claim 5, wherein it has a control device that controls the amount of synthetic fuel entering the heat generation section of the synthetic gas manufacturing apparatus (12) as fuel, so that the synthetic gas manufacturing apparatus (12) or the entire apparatus (10) does not need to be supplied with fuel from the outside.

7. The apparatus (10) of claim 1 or 2, wherein a pipe (64) leads from the hydrogen exhaust pipe (62) of the electrolysis unit (56) to the Fischer-Tropsch synthesis unit (34), a pipe (66) leads from the hydrogen exhaust pipe (62) of the electrolysis unit (56) to the refining unit (36), and a hydrogen input pipe (65) leads from the hydrogen exhaust pipe (62) of the electrolysis unit (56) to the synthesis gas compression unit (43).

8. The apparatus (10) of claim 1 or 2, wherein it has a complete water desalination device (70) having a fresh water inlet pipe (72) and a complete desalination water outlet pipe (74), wherein the complete desalination water outlet pipe (74) is connected to the inlet pipe (58) of the electrolysis device (56), wherein the complete water desalination device (70) has one or more cation and anion exchangers and a membrane device for degassing, so as to desalinate and degas water to a conductivity of less than 20 µS / cm, less than 10 µS / cm, less than 5 µS / cm, or not exceeding 2 µS / cm.

9. The apparatus (10) of claim 8, comprising a water purification device (76) having a process water discharge pipe (80) from the refining device (36) to the water purification device (76), a process water discharge pipe (78) from the Fischer-Tropsch synthesis device (34) to the water purification device (76), and a process water discharge pipe (82) from the syngas production device (12) to the water purification device (76) for purifying water in each device, and further comprising a process water discharge pipe (81) from the carbon dioxide compression device (42) to the water purification device (76), wherein the water purification device (76) is connected to the complete desalination device (70) via a pipe (88) so that water purified by the water purification device (76) can be fed into the complete desalination device (70).

10. The device (10) of claim 9, wherein the water purification device (76) has an anaerobic reactor.

11. The apparatus (10) of claim 1 or 2, wherein a methane steam reformer (31) serves as a second synthesis gas manufacturing apparatus (31) for producing a crude synthesis gas containing hydrogen and carbon monoxide from methane, water and hydrogen, wherein the methane steam reformer (31) has a hydrogen inlet pipe (61), a methane inlet pipe (13), a water (steam) inlet pipe (23), a crude synthesis gas outlet pipe (21), and a process water outlet pipe (85) of the methane steam reformer (31), wherein the hydrogen inlet pipe (61) is connected to the hydrogen outlet pipe (62) of the electrolysis unit (56), and the crude synthesis gas outlet pipe (21) is connected to the crude synthesis gas outlet pipe (20) of the synthesis gas manufacturing apparatus (12).

12. The apparatus (10) of claim 1 or 2, wherein a synthesis gas compression device (43) is provided downstream of the separation device (28) for compressing the synthesis gas to the pressure required for Fischer-Tropsch synthesis, wherein the synthesis gas compression device (43) is connected to the separation device (28) via the synthesis gas discharge pipe (32) and to the Fischer-Tropsch synthesis device (34) via the synthesis gas input pipe (44), wherein the synthesis gas compression device (43) has a hydrogen input pipe (65) connected to the electrolysis device (56).

13. The apparatus (10) of claim 1 or 2, wherein a methanation unit (11) is provided for converting carbon dioxide and hydrogen into methane and water, wherein the methanation unit (11) has a carbon dioxide input pipe (19), a hydrogen input pipe (67) connected to a hydrogen discharge pipe (62) of an electrolysis unit (56), a methane discharge pipe (17), and a process water discharge pipe (87) of the methanation unit (11), wherein the methane discharge pipe (17) is connected to the methane input pipe (14) of the synthesis gas manufacturing unit (12).

14. A method for producing synthesis gas performed in an apparatus (10) as claimed in any one of claims 1 to 13.

15. The method of request item 14, wherein the method does not emit carbon dioxide.

16. The method of claim 14 or 15, wherein the gas produced by the Fischer-Tropsch synthesis unit (34), the gas produced by the refining unit (36), and a portion of the synthetic fuel produced by the refining unit are fed into the heat generation section of the synthesis gas manufacturing unit (12) as fuel, wherein the method is controlled such that the synthesis gas manufacturing unit (12) or the entire equipment (10) does not require external fuel input.

17. The method of claim 14 or 15, wherein a portion of the hydrogen produced by the electrolysis unit (56) is input into the Fischer-Tropsch synthesis unit (34), a portion of the hydrogen produced by the refining unit (36) and a portion of the hydrogen produced by the electrolysis unit (56) are input into the synthesis gas manufacturing unit (12), wherein the H2 / CO-Mohr ratio of the crude synthesis gas produced by the synthesis gas manufacturing unit (12) is controlled to be from 1.15 to 1.

80.

18. The method of claim 14 or 15, wherein a nickel oxide catalyst is added to the synthesis gas manufacturing apparatus (12) for dry reforming, the dry reforming being carried out at a pressure of 10 to 50 bar and a temperature of 700 to 1200°C.

19. The method of claim 14 or 15, wherein a crude synthesis gas containing hydrogen and carbon monoxide is produced from methane, water and hydrogen in a methane steam reformer (31), wherein water (steam), methane and hydrogen from the electrolysis unit (56) are fed into the methane steam reformer (31), while the crude synthesis gas and water are discharged from the methane reformer (31), wherein the crude synthesis gas is fed into the input separation unit (28) and the water is fed into the water purification unit (76), wherein dry reforming is performed in the synthesis gas production unit (12), and the amount of methane used in the dry reformer and the methane steam reformer is adjusted to 30 to 60% to 40 to 65%, and the H2 / CO-Mohr ratio of the crude synthesis gas produced by the dry reformer is adjusted to 1.13 to 1.80, and the H2 / CO-Mohr ratio of the crude synthesis gas produced by the methane steam reformer is adjusted to 3.20 to 3.

60.

20. The method of claim 14 or 15, wherein carbon dioxide and hydrogen from the electrolysis unit (56) are converted into methane and water in a methanation unit (11), wherein the methane is fed into a synthesis gas manufacturing unit (12) and the water is fed into a water purification unit (76).

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