Catalytically produced alkanes

Abstract

The invention relates to a method for producing a mixture of alkanes; a mixture of alkanes which is produced by the method according to the invention; a method for producing methanol; a method for producing methane; a method for producing hydrogen using the alkanes produced according to the invention; and a device for producing a mixture of alkanes.

Description

[0001] Catalytically produced alkanes

[0002] Subject of the invention

[0003] The present invention relates to a process for producing a mixture of

[0004] Alkanes; a mixture of alkanes produced according to the process of the invention; a process for producing methanol; a process for producing methane; a process for producing hydrogen using the alkanes produced according to the invention; and an apparatus for producing a mixture of alkanes.

[0005] State of the art

[0006] In the wake of global efforts to develop sustainable solutions for energy generation and waste management, the conversion of biomass, including organic waste, into bio-based liquid fuels such as oils and diesel, as well as the simultaneous recovery of valuable minerals for fertilizer production, has gained increasing importance. These approaches not only enable the reduction of dependence on fossil fuels by providing renewable energy sources but also promote a closed-loop system by converting waste products into useful and storable resources.

[0007] The catalytic reaction of raw materials and residues to produce middle distillate in so-called reaction turbines is well known. A disadvantage of the invention, and simultaneously the reason for the current low application of this technology, is the high power consumption of the reaction turbines, which heat and mix the input materials with the reaction oil and catalyst. Due to this high power consumption, a large portion of the product produced is reused for electricity generation. Up to 30% of the product produced is reused for electricity generation. A further disadvantage of using reaction turbines is their noise generation and the high regular maintenance costs.

[0008] This patent application describes an efficient and sustainable method for biomass conversion, the core of which is to provide an integrated process for converting biomass into high-quality fuels and feedstock chemicals, and for converting the minerals contained in the biomass into fertilizers. Furthermore, the process according to the present invention is also energy-efficient.

[0009] It is therefore an object of the present invention to provide a process for converting biomass into high-quality fuels and fertilizers, which can be operated in a significantly more energy-efficient manner than the processes known in the prior art.

[0010] Summary

[0011] The inventors of the present invention have found that the high electricity consumption during the conversion of biomass to mixtures of alkanes can be reduced by carrying out the process in an injection stirred tank (1) with injection of air or oxygen. The reduced energy consumption is based on the fact that heating to the process temperature and heating of the starting materials to the process temperature takes place by partial oxidation in the liquid phase, so that the electricity consumption of the process is reduced by at least 95%. The energy required to heat the starting materials from 20°C to the process temperature of 300°C is no longer generated by friction in reaction turbines, but almost exclusively by partial oxidation with a gas containing oxygen, such as air or pure oxygen.

[0012] Therefore, in one aspect, the present invention relates to a process for producing a mixture of alkanes, which comprises at least the following steps:

[0013] (A) reacting biomass with at least one gas containing oxygen in the presence of at least one catalyst in the liquid phase at a temperature in the range of ≥ 270 to ≤ 360 °C, preferably at 300 °C, to obtain a mixture of reaction gas, mixture of alkanes and water vapor, and (B) separating the mixture of alkanes from reaction gas and water vapor by condensation in a product vapor separator (2) to obtain the mixture of alkanes, characterized in that step (A) takes place in an injection stirred vessel (1).

[0014] The process according to the invention is characterized in that the catalyst activates the biomass, i.e. the raw materials and residues. Raw materials and residues can be organic waste, but also plastics such as polyesters, such as PET, and polyalkylenes, such as polyethylene and polypropylene. The oxidation of the biomass forms CO2, which also increases the reaction rate. The biomass is preferably converted in the injection stirred tank (1) within a few minutes, more preferably within > 2 to ≤ 10 minutes. The injection stirred tank is therefore not only the reactor for converting the biomass, but also ensures the provision of energy for the entire process, i.e. the sequence of oxidation, selective condensation of the alkanes, distillation of the alkanes and separation of the reaction gases and condensation of the water vapor.

[0015] The injection stirred vessel (1) comprises a tank (1d), at least one stirrer (1a) and at least two inlets (1b, 1c) for gases, wherein the at least one stirrer (1a) is arranged in the lower region of the tank (1d).

[0016] The injection agitator vessel (1) can be an impact mixer or an impact mixing turbine.

[0017] The conversion of biomass into a mixture of alkanes takes place in a reaction or stirred tank, hereinafter referred to as the injection stirred tank (1). The injection stirred tank (1) is partially filled with a liquid phase consisting of the biomass in liquid form and the catalyst.

[0018] The core of the injection stirred vessel (1) consists of a tank (1d) made of materials such as stainless steel, fiberglass, or special plastics to ensure chemical resistance, purity, and durability. Within the tank (1d) is at least one stirrer (1a), which typically consists of one or more agitators (1a), such as propeller, turbine, paddle, or anchor stirrers, which ensure a homogeneous mixture of the ingredients, preferably the liquid phase. An injection stirred vessel (1) can be constructed in various shapes and sizes to meet the specific requirements of the process. The choice of shape and size of the injection stirred vessel (1) depends on many factors, including the volume of materials to be processed, the type of chemical reaction or mixture, the physical properties of the biomass and catalyst, and the required processing time.

[0019] The injection stirred vessel (1) is preferably cylindrical, spherical, or conical in shape. The injection stirred vessel (1) is preferably cylindrical in shape with a round cross-section. This shape offers a good balance between volume efficiency and surface area for heat exchange and facilitates cleaning and maintenance.

[0020] The stirrer (1a) is preferably a propeller, turbine, paddle, or anchor type stirrer. The stirrer (1a) ensures optimal mixing of the liquid phase with the gas. Propeller stirrers consist of two or more blades attached to a central axis. They rotate rapidly and generate an axial flow that moves liquids along the axis of the tank (1d). Propeller stirrers are preferred for mixing low-viscosity liquids and dispersing gases in liquids. Turbine stirrers are also preferred. Turbine stirrers consist of several flat or curved blades arranged radially around a central axis. They generate a radial flow that propels liquids across the tank (1d), ensuring intensive mixing. Other preferred stirrers are paddle or anchor type stirrers.Paddle impellers have a simple design with one or more flat blades mounted perpendicular to the impeller axis. They typically move slowly and produce gentle, low-shear mixing. Anchor impellers have large, flat blades that follow the inner contour of the tank ( 1 d). They rotate slowly and ensure thorough mixing by scraping the tank walls, preventing the formation of dead zones.

[0021] The injection stirred vessel further comprises at least two inlets (1b, 1c). Inlets for gases into a tank (1d) are specially designed openings or devices that allow the controlled introduction of gases or gaseous substances into the interior of a tank (1d). The inlets can be in the form of spargers, gas injection nozzles, and vent valves. A sparger is a device attached to the bottom or side of a tank (1d) to introduce gas directly into the liquid. A sparger disperses the gas into fine bubbles, thereby maximizing the contact area between gas and liquid and increasing the efficiency of gas exchange. Gas injection nozzles are designed openings that introduce the gas into the tank (1d) in specific patterns or under specific pressure conditions. They can be designed to inject the gas in the form of a targeted jet or a diffused pattern for broad distribution.Vent valves allow the controlled inlet and outlet of gases to regulate the pressure within the tank (1d) or to create a specific atmosphere. These valves can be controlled manually or automatically to respond to changes in the process.

[0022] In a preferred embodiment, one of the at least two inlets (1b) is arranged above the stirrer (1a), and one of the at least two inlets (1c) is arranged below the stirrer (1a). Preferably, the at least one gas containing oxygen is sucked in via the at least one first inlet (1b), the gas being preheated, and the at least one gas containing oxygen is preferably supplied under pressure via the at least one second inlet (1c). The air is preheated in the upper part without pressure and is connected to the intake of hot air above the stirrer (1a) in the injection stirred vessel (1). In the lower part, the gas is supplied under pressure from the compressor, which injects the air below the stirrer (1a) via a bubble ring.

[0023] In a preferred embodiment, the injection-stirred vessel (1) has a double jacket containing a thermal oil. The double jacket encloses the injection-stirred vessel and is designed for the circulation of thermal oil. The double jacket is constructed to offer an optimal geometric shape that maximizes heat transfer efficiency. The geometric configuration of the double jacket is precisely matched to the dimensions of the tank (1d) to ensure even distribution of the thermal oil around the interior of the tank (1d). The thermal oil filled in the double jacket was specifically selected to offer high thermal conductivity and stable thermal performance over a wide temperature range. These properties of the thermal oil enable fast and even heat transfer. The selection of the thermal oil is based on its ability to efficiently absorb and release heat.

[0024] In a preferred embodiment, the at least one catalyst is a cation aluminum silicate. Cation aluminum silicates are zeolites. Zeolites are microporous, crystalline aluminosilicates consisting of a three-dimensional framework of SiO4 and AlO4 tetrahedra connected by oxygen atoms. The substitution of Si(IV) by Al(III) in the crystal lattice leads to a negative charge, which can be neutralized by the uptake of cations such as Na + , K + , Ca 2+ These cations are exchangeable, which gives zeolites the ability to selectively adsorb or desorb molecules based on their size and electrical charge. The zeolites, i.e., the cation aluminum silicate, ensure the specific conversion of biomass into mixtures of alkanes.

[0025] In a preferred embodiment, a small portion of the liquid phase is continuously recycled during the process in an inert gas vacuum evaporator (7), with a solid residue being separated off. The inert gas vacuum evaporator (7) is heated with thermal oil via the injection stirred vessel (1) and is under vacuum, whereby the appropriate amount of the liquid phase for recycling is sucked in via a valve. The partial pressure of the liquid phase is reduced by means of an inert gas and the adjustment of the vacuum. This results in the liquid phase evaporating almost completely even at 300°C, leaving the inorganic components at the bottom. These inorganic components are suspended in water according to the present invention. The insoluble catalyst substance calcium aluminum silicate is separated out in the water circuit and fed into the plant's input system.After purification, the brine is evaporated in selective electrolysis and can be used as fertilizer. Selective electrolysis uses low voltages to separate metallic contaminants, such as those from pharmaceuticals, at electrodes and use them as a product.

[0026] In a preferred embodiment, the injection-stirred vessel (1) comprises at least one outlet (1e). The mixture of reaction gas, mixture of alkanes, and steam is preferably introduced into the injection zone of the product vapor separator (2) via at least one outlet (1e) and a 180° bend (2a) and at least one heat exchanger (2b), preferably two heat exchangers (2b), in order to reduce the temperature for the subsequent selective condensation to 100°C. Condensation preferably takes place in the product vapor separator (2) at a temperature in the range of ≥ 90 to 110°C, preferably at 100°C. The catalytically produced mixture of reaction gas, mixture of alkanes, and steam passes through a falling pipe into the injection zone of the product vapor separator (2), which condenses the mixture of alkanes but allows the steam and other reaction gases to pass through.For this purpose, the product from the lower connecting pipe between this partial condensation and the distillation is injected to lower the temperature to 100°C. If necessary, additional condensed water is injected. This ensures that only the product (i.e., the mixture of alkanes) remains in the product vapor separator (2), while the water vapor and other reaction gases leave the vessel. This causes an increasing amount of a mixture of alkanes to form in the product vapor separator (2). The lower section of the product vapor separator (2) is connected to the product distillation vessel (3), which is heated in the upper section with thermal oil. When the fill level reaches this upper heated zone, the clean mixture of alkanes evaporates. Due to its chemical structure with the side chains, the mixture of alkanes also has a lower evaporation temperature of approximately 200°C.As a result, the thermal oil heating of the jacket on the product distillation vessel (3) is entirely sufficient to evaporate the alkane mixture. Additionally, after condensation in the column and condenser, a vacuum system is connected to the product tank of the distillation system, which supports the evaporation of the alkane mixture and enables a lower evaporation temperature. The product distillation vessel (3) is heated via the injection stirred vessel (1) and a corresponding thermal oil jacket device for a thermal oil circuit between the jacket of the injection stirred vessel (1) to the upper part of the product distillation vessel (3) and the first part of the column of the distillation system. The temperature of the thermal oil, which is almost 300 °C in the injection stirred vessel (1), ensures the continuous distillation of the alkane mixture.The injection-stirred tank (1) also has an inlet screw conveyor that feeds the biomass from above via a feed shaft to below the liquid level of the liquid phase in the tank (1d). The stirrer (1a) captures the biomass and mixes it in the liquid phase. The residence time of the biomass in the injection-stirred tank (1) from its inlet until its chemical decomposition and conversion into alkanes, water vapor, and reaction gas is a few minutes, depending on the amount. If the biomass contains acid-forming substances, these are neutralized by the additional addition of approximately 1% limestone (CaCO3).

[0027] The water vapors extracted from the product vapor separator (2) and other reaction gases from the partial oxidation enter a water condensation tank (5), where they are separated into liquid water and inert gas by air-cooled circulating water and the injection of this water for condensation. A small portion of the inert gas is drawn in by the inert gas vacuum evaporator (7) and the majority is released to the outside after being purified via a ceramic filter (6).

[0028] The condensed water from the water condensation tank (5) flows into a product water tank (4), which is slightly underpressured by a vacuum pump via the ceramic filter (6). A floating layer of alkanes forms in this product water tank (4), which condenses at temperatures below 100°C. This fraction is separated by gravity and fed via a liquid pump to the feed system or distillation system in the lower connecting pipe.

[0029] The process according to the invention enables the partial oxidation of biomass, such as organic waste and plastics, such as polyesters including PET and polyalkylenes including polyethylene and polypropylene, to a mixture of alkanes.

[0030] In a further aspect, the present invention therefore relates to a mixture of alkanes having the formula CnH2n+2, where n = 14, 15, 16, 17, 18, 19, 20, 21, 22, or 23. Preferably, n is on average 17. The molecular length of the alkanes, i.e., the number n, varies with the process temperature.

[0031] The mixture of alkanes obtained by the process according to the invention can be further converted to methanol, methane, or hydrogen. The conversion takes place in a downstream tube-bundle pressure reactor (8), which is heated with the thermal oil via the injection stirred vessel (1). The tube-bundle pressure reactor (8) contains a tube coil running from top to bottom and, after a dividing wall with a passage, from bottom to top. The thermal oil, at approximately 300°C, is passed in countercurrent around the tube coils, heating them accordingly. The tube coils contain a knitted aluminum mesh coated with the catalyst CuZnOAhOa, which was applied by impregnation and subsequent calcination.The mixture of alkanes is then mixed with water and suspended aluminum silicate, preferably cation aluminum silicate, to activate the carbon, pumped into the tube bundle at a pressure of 200 bar and finally, after cooling, expanded in the following heat exchanger and cooler.

[0032] Accordingly, the present invention also relates to a process for producing methanol, wherein the mixture of alkanes according to the invention is reacted with water according to the formula CnH2n+2 + nx H2O = nx CH3OH, where n = 14, 15, 16, 17, 18, 19, 20, 21, 22 or 23.

[0033] The present invention also relates to a process for producing methane, wherein a mixture of alkanes obtained according to the invention is reacted with water according to the formula 2CnH2n+2 + 2 x 1.5 nx H2O = 2n x CH4 + n CO2, where n has the meaning given above.

[0034] The present invention also relates to a process for producing hydrogen, wherein the mixture of alkanes according to the formula C n H2n+2 + 2n x H2O = 3n x H2 + n CO2, where n has the meaning given above.

[0035] The desired product can thus be determined by adjusting the mixing ratio of alkanes to water. The length of the reactor and the mixing ratio with the catalyst increase from the production of methanol to the production of methane to hydrogen to ensure the complete conversion of the mixture of alkanes. In a further aspect, the present invention relates to a mixture of alkanes having the formula C n H2n+2, where n = 14, 15, 16, 17, 18, 19, 20, 21, 22 or 23, which have a density at 15 °C in the range of ≥ 740 to ≤ 850 kg / m 3, determined according to DIN EN ISO 12185:1997, and a flash point in the range of ≥ 30 to ≤ 65 °C, determined according to DIN EN ISO 2719:2021, and a sulfur content in the range of ≥ 5 to ≤ 500 mg / kg, determined according to DIN EN ISO 20884:2022, and an acid number in the range of ≥ 100 to ≤ 110 mg KOH / g, determined according to DIN EN ISO 14104:2003.

[0036] Furthermore, the mixture of alkanes preferably has a kinetic viscosity in the range of ≥ 1.8 2 / s up to 8.8 mm 2 / s, determined according to DIN EN ISO 3104:2021. Furthermore, the mixture of alkanes preferably has a cold filter plugging point (CFPP) in the range of ≥ -30 °C to ≤ -10 °C, determined according to DIN EN 116:2018. Furthermore, the mixture of alkanes according to the invention preferably has a cetane number (ICN) in the range of ≥ 45 to ≤ 65, determined according to DIN EN 17155:2018. Likewise preferably, the mixture of alkanes according to the invention preferably has a sulfate ash content (775 °C) of <0.005% (m / m), determined according to ISO 3987:2010. Furthermore, the mixture of alkanes according to the invention preferably has a water content in the range of ≥ ≤ 3600 mg / kg, preferably even ≤ 200 mg / kg, determined according to DIN 51777 Verf. A:2020. Furthermore, the mixture of alkanes according to the invention preferably has an alkali content (Na+K) of <1.0 mg / kg, determined according to DIN EN 14538:2006 and a metal content II (Ca+Mg) of <1.0 mg / kg, determined according to DIN EN 14538:2006.Furthermore, the mixture of alkanes according to the invention preferably has a cloud point in the range from ≥ -15 °C to ≤ -5 °C, determined according to DIN EN 23015:1994.

[0037] In a further aspect, the present invention also relates to a device for producing a mixture of alkanes comprising at least one injection stirred vessel (1) which comprises a tank (1d), at least one stirrer (1a), at least one outlet (1e) and at least two inlets (1b, 1c) for gases, wherein the at least one stirrer (1a) is arranged in the lower region of the tank (1d), at least one of the two inlets (1b) is arranged above the stirrer (1a), and one of the at least two inlets (1c) is arranged below the stirrer (1a), and a product vapor separator (2), wherein the heat exchangers (2b) are arranged between the at least one outlet (1e) and the product vapor separator (2).

[0038] In a preferred embodiment of the device, the at least one gas containing oxygen is sucked in via the at least one first inlet (1b), the gas being preheated by heat exchangers (2b), and the at least one gas containing oxygen is supplied under pressure via the at least one second inlet (1c), the second inlet (1c) being connected to a heat exchanger (2c) and an air compressor (1f).

[0039] The preferred embodiments of the method described above and below also relate to the device.

[0040] Detailed description of the embodiments

[0041] The following reference numerals are used in Fig. 1 and Fig. 2. Fig. 1 shows a left part of the system according to the invention that is essential to the invention, and Fig. 2 shows a right part of the system according to the invention that is essential to the invention, wherein the respective connection is identified by the letters a, b, c, d and e.

[0042] List of reference symbols:

[0043] 1 injection stirred tank

[0044] 1a stirrer

[0045] 1 b Inlet

[0046] 1c entrance

[0047] 1d Tank

[0048] 1st outlet

[0049] 1f Air compressor Product vapor separator a Bend 2b Heat exchanger

[0050] 2c heat exchanger

[0051] 3 product distillation vessels

[0052] 4 Product water tank

[0053] 5 water condensation tanks

[0054] 6 ceramic filters

[0055] 7 inert gas vacuum evaporators

[0056] 8 tube bundle pressure reactor

[0057] The injection stirred tank (1) has a hot air input through the stirrer from the upper part of the heat exchanger above the selective condensation of the product vapor separator (2), as well as via a compressor which is connected to the lower part of the heat exchanger above the product vapor separator (2) and blows in the air below the stirrer.

[0058] This vessel, the product vapor separator (2) for selective condensation with the product injection system and, in the case of superheating, additional product water, contains a demister that ensures that the alkane mixture is recovered in liquid form and collects at the bottom of this vessel. This bottom of the product vapor separator (2) for selective condensation is connected by a connecting pipe to the product distillation vessel (3) (partial rectification), from which the product injection for the product vapor separator (2) also takes place via a pump.

[0059] The level in the product vapor separator (2) increases due to production and thus also causes the level in the product distillation vessel (3) to rise, which causes evaporation when the fill level is appropriate.

[0060] The compressor for the blown-in air is located between the product distillation tank (3) and the product vapor separator (2) for selective condensation. This compressor is equipped with two molecular sieves for pressure swing adsorption in the event of oxygen enrichment. Above the product water tank (4), the water content is separated from the inert gas from the product vapor separator (2) by injecting cooled water into the water condensation tank (5).

[0061] The product water tank (4) features a gravity separation system for product separation from the remaining alkane mixture, which is then separated and fed into the feed system of the injection stirred tank (1) or the product distillation tank (3). A small portion of the inert gas separated from the water passes through a ceramic filter (6) into the inert gas vacuum evaporator (7), and the majority is released into the atmosphere.

[0062] The portion of inert gas drawn into the inert gas vacuum evaporator (7) is heated by the partial cooling of the product of oil vapor and inert gas drawn off from the inert gas vacuum evaporator (7) in a subsequent heat exchanger. A cooler is connected downstream of this heat exchanger.

[0063] The inert gas vacuum evaporator (7) thus separates the oil fraction, which is returned to the plant, from the inorganic granulate accumulating at the lower end. This granulate passes through the screw feeder at the lower end into the container located below, which separates the fertilizers / mineral salts from the catalyst. This is achieved with the water supplied from the product water tank (4), which separates the insoluble part, the catalyst for recycling, from the brine. The fertilizers / mineral salts are extracted from the brine after selective electrolysis and evaporation.

[0064] When processing waste biomass, the most commonly available input material (raw and residual material), the resulting fertilizer contains all the minerals extracted from the soil by the plant. This also allows the present invention to optimize the fertilizer issue. Biomass produced by solar energy (formation of cellulose via photosynthesis) is stored in the form of a mixture of alkanes, and the minerals extracted from the soil can be returned to the arable land or forest. Examples

[0065] The present invention is illustrated below using examples. These examples are intended solely to illustrate the invention and are in no way intended to limit the scope of the invention.

[0066] [sEpjA 500 kW generator heats the thermal oil of the heating jacket of a stirred injection tank (1) and the reaction oil contained therein to 300°C through heat exchange and electrical heating. This heating takes 30-40 minutes for a stirred injection tank (1). The heating via the generator is then stopped, and the air intake and injection into the stirred injection tank (1) takes over the further heating and heating of the raw and residual materials such as wood, crop residues, and plastics introduced via an input system through partial oxidation into the liquid phase. The production capacity of one stirred injection tank (1) is designed for 500 liters / h of alkane mixture and is achieved by sucking in 250 cubic meters of air per hour through the stirrer and 250 cubic meters of air per hour via the air compressor.

[0067] After increasing the temperature to 330 °C, a second injection stirred tank (1) can be heated to operating temperature by using thermal oil from the jacket of the first tank via a circulating pump to heat the second injection stirred tank (1). The capacity of a plant can thus be increased from one injection stirred tank (1) with 500 liters per hour to 5000 liters per hour of an alkane mixture with 10 injection stirred tanks (1). For this purpose, 3-5 injection stirred tanks (1) are connected to a product vapor separator (2) (selective condensation) and a subsequent product distillation tank (3) (partial rectification). The electrical power of the stirrer of one injection stirred tank (1) is 40 kW, meaning that the generator supplies a total of 400 kW for the stirrers when operating 10 injection stirred tanks (1). The remaining 100 kW is consumed by the pumps and electronics.

[0068] Thus, the three product distillation vessels (with ten injection stirred vessels) each deliver 1,500 to approximately 1,700 liters per hour of alkane mixture. One injection stirred vessel (1) is located in the purification stage with the inert gas vacuum evaporator (7). Depending on the input material, an additional 2,000 liters of condensation water are produced per hour. During the subsequent conversion of the product into the other products methanol, methane, and hydrogen, a portion of the produced alkane mixture is homogeneously mixed with the respective proportion of water, i.e., with the same amount of water (1:1) for methanol, 1.5 times the amount of water for methane, and twice the amount of water for hydrogen, using the cation aluminum silicate catalyst, and then injected into the tube bundle in the tube bundle pressure reactor (8) via a pressure pump.The circulating thermal oil provides heating for the endothermic reaction, and downstream of the tube-bundle pressure reactor (8) is a heat exchanger for heating the injected liquid mixture and a cooler. The catalyst settles downstream of the cooler and is recycled.

[0069] An exemplary embodiment of the device will describe the invention in more detail. The injection stirred tank (1) has a diameter of 1,200 mm and a stirrer with a diameter of 400 mm. A flow ring with a diameter of 600 mm is attached around the stirrer. The stirrer is connected to a 40 kW electric motor. At the upper end of the injection stirred tank (1) there is an inlet pipe with a diameter of 150 mm, which is connected on the inlet side to a screw system with a hopper and on the tank side to a 200 mm pipe which projects 1,500 mm long into the 2,500 mm high tank. At the outlet side of the injection stirred tank (1) there is an upward pipe with a diameter of 300 mm, which leads 1,500 mm upwards and then has a 180° bend downwards. Connected to this is the pressureless air preheater with finned tubes, with the fins on the air side.The heat exchanger connected afterwards is pressure tested to 1 bar overpressure and also has finned tubes with fins on the air side.

[0070] The product vapor separator (2) has a demister in the center, which is attached to a 500 mm diameter pipe with a diameter of 300 mm. The product vapor separator (2) has a diameter of 1,800 mm and a height of 3,000 mm. A connecting pipe with a diameter of 150 mm is attached at the lower end. The injection nozzles (for cooling) of the product produced in this vessel are designed for 1,000 liters of product per hour and 200 liters of water per hour. The product distillation vessel (3) has a vessel diameter of 1,000 mm and a column diameter of 300 mm. The column is filled with loose packing. The height of the distillation system on the product distillation vessel (3) is 2,500 mm.

[0071] The water condensation tank (5) is designed for 2,000 liters of water per hour and has a 2,000 kW recooler. The adjoining product water tank (4) has a diameter of 1,200 mm. At its lower end, it has a gravity valve that opens when the liquid density falls below 0.95 kg / liter and then closes (returning the product to the distillation). The inert gas vacuum evaporator (7) is located downstream of the injection stirred tank (1). It has a diameter of 800 mm and a height of 2,000 mm. It is pressure-tight, and a 40 kW gear motor for the stirrer is attached to its upper end. At its lower end, a pressure-tight screw lock is attached, which sits on a 300-liter water tank.This water tank is connected to a commercially available screening machine, which drains the insoluble catalyst on the screen into an intermediate tank equipped with a feed pump to the feed screw on the injection agitator tank (1). The circulating water, which forms a brine with the granules, is fed into an evaporator connected to the exhaust gas of the power generator and heated. There, the fertilizer granules are produced. The brine can be passed through selective electrolysis beforehand.

[0072] The device thus consists of five main elements (1-4 and 7) and the necessary auxiliary elements. To produce 5,000 liters / h of alkane mixture, this requires ten injection stirred tanks, three product vapor separators, three product distillation tanks, and a water scrubber and water condenser. An inert gas vacuum evaporator (7) with additional elements is also required to treat the reaction oil and maintain its constant composition. The tube bundle for the subsequent conversion of the alkane mixture to methanol, methane, and hydrogen in the shell-and-tube pressure reactor (8) consists of a top-to-bottom winding pipe with a diameter of 2 inches and a height of 3 meters. At the lower end, there is a connecting line to a bottom-to-top winding pipe. The two sections of the heated shell-and-tube pressure reactor (8) are separated by a partition wall open at the bottom, which ensures the counterflow of the thermal oil.At the end is the preheater for the input mixed product and an aftercooler with a fan. This is followed by the expansion valve with a subsequent cyclone for catalyst separation.

[0073] The mixture of alkanes produced by the process according to the invention was analyzed. The results of the analysis are shown in Table 1.

[0074] Tab. 1 Analysis of the mixture of alkanes

Claims

Patent claims 1 . A process for preparing a mixture of alkanes comprising at least the steps: (A) reacting biomass with at least one gas containing oxygen in the presence of at least one catalyst in the liquid phase at a temperature in the range of 270 to 360 °C, preferably at 300 °C, to obtain a mixture of reaction gas, mixture of alkanes and water vapor, and (B) separating the mixture of alkanes from reaction gas and water vapor by condensation in a product vapor separator (2) to obtain the mixture of alkanes, characterized in that step (A) takes place in an injection stirred vessel (1).

2. Method according to claim 1, characterized in that the injection stirred vessel (1) comprises a tank (1d), at least one stirrer (1a) and at least two inlets (1b, 1c) for gases, wherein the at least one stirrer (1a) is arranged in the lower region of the tank (1d).

3. The method according to claim 2, characterized in that one of the at least two inlets (1 b) is arranged above the stirrer (1 a) and one of the at least two inlets (1 c) is arranged below the stirrer (1 a).

4. Method according to claim 3, characterized in that the at least one gas containing oxygen is sucked in via the at least one first inlet (1b), the gas being preheated, and the at least one gas containing oxygen is supplied under pressure via the at least one second inlet (1c).

5. Process according to one of claims 1 to 4, characterized in that the at least one catalyst is an aluminum silicate, preferably a cation aluminum silicate.

6. Method according to one of claims 1 to 5, characterized in that the injection stirred tank (1) comprises at least one outlet (1e).

7. Process according to one of claims 1 to 6, characterized in that the mixture of reaction gas, mixture of alkanes and water vapor is fed to the product vapor separator (2) via the at least one outlet (1e), a bend (2a) and at least one heat exchanger (2b).

8. Process according to one of claims 1 to 7, characterized in that the condensation takes place in a product vapor separator (2) at a temperature in the range of ≥ 90 to ≤ 110 °C, preferably at 100 °C.

9. Process according to one of claims 1 to 8, characterized in that the mixture of alkanes is a mixture of alkanes having the formula CnH2n+2, where n = 14, 15, 16, 17, 18, 19, 20, 21, 22 or 23, preferably n = 17.

10. Process according to one of claims 1 to 9, characterized in that the liquid phase is recycled in an inert gas vacuum evaporator (7), whereby a solid residue is separated. 11 . Mixture of alkanes with the formula C n H2n+2, where n = 14, 15, 16, 17, 18, 19, 20, 21, 22 or 23, obtained by the process according to any one of claims 1 to 10.

12. Mixture of alkanes with the formula CnH2n+2, where n = 14, 15, 16, 17, 18, 19, 20, 21, 22 or 23, which has a density at 15 °C in the range of ≥ 740 to ≤ 850 kg / m 3 , determined according to DIN EN ISO 12185:1997, and a flash point in the range of ≥ 30 to ≤ 45 °C, determined according to DIN EN ISO 2719:2021, and a sulfur content in the range of ≥ 5 to ≤ 500 mg / kg, determined according to DIN EN ISO 20884:2022, and an acid number in the range of ≥ 100 to ≤ 110 mg KOH / g, determined according to DIN EN ISO 14104:2003.

13. A process for the preparation of methanol or methane or hydrogen, characterized in that the mixture of alkanes according to claim 11 or 12 with water according to the formula C nH2n+2 + nx H2O = nx CH3OH, where n = 14, 15, 16, 17, 18, 19, 20, 21, 22 or 23, or the mixture of alkanes according to claim 11 or 12 with water according to the formula 2 C n H2n+2 + 2 x 1.5 n x H2O = 2n x CH4 + n CO2, where n = 14, 15, 16, 17, 18, 19, 20, 21, 22 or 23, or the mixture of alkanes according to claim 11 or 12 is reacted with water according to the formula CnH2n+2 + 2n x H2O = 3n x H2 + n CO2, where n = 14, 15, 16, 17, 18, 19, 20, 21, 22 or 23 14. Apparatus for producing a mixture of alkanes comprising at least one injection stirred vessel (1) which comprises a tank (1d), at least one stirrer (1a), at least one outlet (1e) and at least two inlets (1b, 1c) for gases, wherein the at least one stirrer (1a) is arranged in the lower region of the tank, at least one of the two inlets (1b) is arranged above the stirrer (1a), and one of the at least two inlets (1c) is arranged below the stirrer (1a), and a product vapor separator (2), wherein the heat exchangers (2b) are arranged between the at least one outlet (1e) and the product vapor separator (2).

15. Device according to claim 14, characterized in that the at least one gas containing oxygen is sucked in via the at least one first inlet (1b), the gas being preheated by heat exchangers (2b), and the at least one gas containing oxygen is supplied under pressure via the at least one second inlet (1c), the second inlet (1c) being connected to a heat exchanger and air compressor (1f).

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