Reactor and method for the thermal cracking of hydrocarbon-containing fluids

Abstract

The present invention relates to a reactor and a method for at least the thermal decomposition of a hydrocarbon-containing fluid to at least produce at least a hydrogen-containing fluid, the reactor comprising a reactor casing, a reactor shaft arranged in the reactor casing, and a reactor lining between the reactor casing and the reactor shaft for at least thermally sealing the reactor shaft from the reactor casing, the reactor shaft having an at least rectangular shape in cross section, and at least one respective electrode for generating thermal energy being arranged on two opposite side walls of the reactor shaft.

Description

[Technical Field]

[0001] The present invention relates to a reactor and a method for at least the thermal decomposition of a hydrocarbon-containing fluid for at least the production of at least a hydrogen-containing fluid, the reactor having a reactor shell and a reactor shaft arranged in the reactor shell, with a reactor lining arranged between the reactor shell and the reactor shaft for heat sealing of the reactor shaft to the reactor shell. The present invention further relates to a method for the thermal decomposition of at least a hydrocarbon-containing fluid for the production of at least a hydrogen-containing fluid, the hydrocarbon-containing fluid being fed to the reactor shaft of the reactor in countercurrent to a moving bed of particles in the reactor. [Background technology]

[0002] It is a basic knowledge that the powerful endothermic reactions known to occur in the chemical industry, for example in the cracking of mineral oil fractions or the reforming of natural gas or naphtha, require temperatures in the range of 500 to 1700 °C to allow sufficient chemical cracking. The reason for this is the thermodynamic limit of equilibrium conversion. The thermal cracking of hydrocarbons also requires high temperatures, especially in the range of 800 to 1600 °C. For methane cracking in particular, such high temperatures are also required to achieve sufficiently high conversions, advantageously above 50%, within a very short time due to the thermodynamic equilibrium and reaction rates.

[0003] The prior art discloses different solutions that provide high temperatures to enable pyrolysis processes. For example, U.S. Patents 2,389,636 and 2,600,076, as well as U.S. Patents 5,486,216 and 6,670,058, describe the use of a solid bed as a heat transfer medium. However, it should be noted that this can lead to adverse surface effects such as adhesion, clumping, and abrasion.

[0004] Oxidative processes as heat sources are described, for example, in German Patent No. 600 16 59T or U.S. Patent No. 3,264,210. The drawbacks of direct use of oxidative processes include, for example, the introduction of foreign substances into the reaction zone, which can contaminate the product. There is also the risk that carbon will be burned off in an undesirable manner, or that the reactant stream will also be burned.

[0005] US Patent No. 2,799,640 or German Patent No. 1 266 273 each disclose an electric heat source, where the drawback is considered to be the uneven heating of the reaction zone, and this instability of the electrical heat input leads to unevenness within the reaction space in pyrolysis, especially in the pyrolysis of methane to produce hydrogen and pyrolytic carbon (CH4<->C+2H2).

[0006] The pyrolysis of methane is a highly endothermic reaction that occurs in a kinetically and thermodynamically favorable manner within a temperature range of approximately 1000°C and pressures up to 40 bar. In addition to hydrogen (H), the thermal cracking also produces pyrolytic carbon (C), which is a further valuable product. The hydrogen and pyrolytic carbon are advantageously further processed or further used to serve as transportation fuels or as combustion fuels in other drive systems, plants, or industrial sectors.

[0007] It is considered basic knowledge that beds of particles, especially beds of carbon particles, are also used for pyrolysis, on which carbon-containing gases such as methane are pyrolyzed. Electrical input of heat, especially by resistive heating, is advantageously suited to providing the reaction enthalpy.

[0008] When a carbon bed is used, electrical current introduced into the reaction space, for example through the use of an electrode or electrode pair, flows through the bed and is dissipated into heat energy due to the electrical resistance of the particle bed. The electrical resistance arises from contact points between the bed particles and low-transfer regions, but carbon particles have high electrical conductivity. Essentially uniform heat input to the heating zone of the reaction space requires at least intermittently uniform electrical resistance across the entire cross-sectional area of ​​the reaction space. However, it is known that paths with different electrical resistance always occur, such that current preferentially flows through areas of lower electrical resistance. As a result, pyrolytic carbon deposition in these regions increases, resulting in further reductions in resistance along these lower-resistance paths. This results in localized hot spots, localized sudden drops in electrical resistance, blockages, and ultimately non-uniformities that lead to heating failure. In-house research has shown that known reactors, particularly known reactor geometries (particularly known reaction space geometries), and known pyrolysis processes, such as methane, result in carbon formation in a central location within the reaction space, with said formation extending at least partially centrally along the vertical longitudinal direction of the reaction space. This carbon formation consists of coalesced carbon particles, which indicates that the pyrolysis that took place was mainly only in the center of the reaction space, and not over the entire cross section of the reaction space. [Prior art documents] [Patent documents]

[0009] [Patent Document 1] U.S. Patent No. 2,389,636 [Patent Document 2] U.S. Patent No. 2,600,07 [Patent Document 3] U.S. Patent No. 5,486,216 [Patent Document 4] U.S. Patent No. 6,670,058 [Patent Document 5] German Patent No. 600 16 59T [Patent Document 6] U.S. Patent No. 3,264,210 [Patent Document 7] U.S. Patent No. 2,799,640 [Patent Document 8] German Patent No. 1 266 273 Summary of the Invention

[0010] The causes of the non-uniformity in the known reaction space and known pyrolysis process, and the resulting failure of the known reactor heating concept, have been the subject of in-house research by the applicant. It has been discovered that a pronounced radial temperature profile exists due to the high ratio of the wall area of ​​the reaction space to the reaction volume of the reaction space. Higher temperatures in the center of the reaction space result in higher conversion rates, i.e., higher carbon deposition on the bed particles, which in turn results in greater carbon deposition from carbon-containing gases, such as methane gas. This results in lower electrical resistance in this region, resulting in an associated preferential current flow in the region of lower electrical resistance.

[0011] It is therefore an object of the present invention to at least partially remedy the above-mentioned drawbacks of known reactors and pyrolysis methods. In particular, it is an object of the present invention to provide a reactor and method for the pyrolysis of at least hydrocarbon-containing fluids, which in a simple and inexpensive manner allows for essentially uniform heating of the reactor shaft over its cross section (reaction space), and thus allows for the creation and maintenance of an electric field that is at least intermittently uniform in part and has a corresponding at least intermittently uniform resistance in part.

[0012] The above object is achieved by a reactor for the thermal cracking of hydrocarbon-containing fluids having at least the features of claim 1, and a method for the thermal cracking of hydrocarbon-containing fluids having at least the features of claim 7. Further features and details of the invention will become apparent from the dependent claims, the description and the drawings. The features and details described in relation to the reactor of the invention are naturally also applicable in relation to the method of the invention, and vice versa, so that reference is always made to alternative subject matter with respect to the disclosure relating to the individual aspects of the invention, or alternative subject matter can be referred to. Furthermore, the method of the invention can be carried out using the reactor of the invention.

[0013] The reactor of the present invention, for at least the thermal decomposition of a hydrocarbon-containing fluid to at least produce at least a hydrogen-containing fluid, comprises a reactor shell and a reactor shaft disposed within the reactor shell. A reactor lining for thermally sealing the reactor shaft to the reactor shell is disposed between the reactor shell and the reactor shaft. According to the present invention, the reactor shaft has an at least rectangular cross-section, and at least one electrode for generating thermal energy is disposed on each of two opposing side walls of the reactor shaft. It is further contemplated that the reactor lining also serves as electrical insulation to prevent the electrical energy generated by the electrodes from being released into the environment outside the reactor. Fluid in the context of the present invention is also understood to mean gas or liquid. Thus, the hydrocarbon-containing fluid can be, for example, methane (methane gas), natural gas, or blue gas. Therefore, the term "hydrocarbon-containing fluid" in the context of the present invention is understood to mean any fluid (gas / liquid) containing hydrocarbons that can be dissociated into carbon and hydrogen by a pyrolysis method. The reactor shell of the reactor advantageously has an annular / circular cross-section. This is particularly advantageous for withstanding high pressures. However, it is also conceivable that the reactor shell, compared to the reactor shaft, which may also be referred to as the reaction space, has at least a rectangular cross-sectional geometry, particularly preferably a geometry that corresponds to the geometry of the reactor shaft. The reactor shaft can also advantageously have a rectangular cross-sectional geometry, particularly a square geometry. However, it is also conceivable that the reactor shaft has a polygonal cross-section, particularly a polygonal cross-section with a pentagon or higher polygonal shape. Particularly advantageously, there are at least two opposing walls, particularly inner walls, that are parallel and opposite to each other when viewed in cross section of the reactor shaft. Electrodes for generating a partially at least intermittently uniform electric field, particularly an essentially uniform electric field, are arranged on these parallel and opposing walls of the reactor shaft. Advantageously, the electrodes are also opposite each other, i.e., at the same height when viewed in the longitudinal direction of the reactor shaft. Particularly advantageously, the electrodes are arranged inside the side walls of the reactor shaft. The electrode arrangement advantageously provides direct electrical resistance heating of the particles of the moving bed, particularly of the particle bed.The quadrangular, in particular rectangular, especially square, geometry of the reactor shaft and the correspondingly described electrode arrangement allow the creation of an at least intermittently uniform potential field between the mutually opposing electrodes, which in addition prevents any slippage of the material flow and the associated reduction in conversion.

[0014] The particles of the moving bed may have a size of 0.5 mm to 20 mm, preferably 1 mm to 10 mm. The process for pyrolysis of hydrocarbon-containing fluids is advantageously carried out at a pressure of 1 bar to 50 bar, preferably 5 bar to 30 bar. The temperatures produced here are mainly between 800°C and 1600°C, preferably between 1000°C and 1400°C.

[0015] In one embodiment, the mutually opposing electrodes are at least partially centered in the reactor shaft when viewed in the vertical longitudinal direction of the reactor. This means that at least a portion of each electrode contacts or extends to the (theoretical) centerline of the reactor (seen at the midpoint of the longitudinal reactor / longitudinal cross section), while the remaining portion of each electrode is located in a reactor shaft region below or above this theoretical centerline. More specifically, each electrode is considered to be located in a portion of the reactor shaft facing the head of the reactor or in a region of the reactor shaft facing the bottom (base) of the reactor. However, alternatively, each electrode may be located exactly in the center of the reactor shaft (longitudinally / longitudinal cross section). Alternatively, none of the electrodes of an electrode pair may be located in the center of the reactor shaft at least in a portion of the wall or side wall of the reactor shaft when viewed in the vertical longitudinal direction of the reactor. Instead, the electrodes are located only in the reactor shaft region below or above this theoretical centerline on the reactor shaft wall.

[0016] In one embodiment, there are at least two or more electrodes for generating thermal energy, each located on two opposing side walls of the reactor shaft. Advantageously, there are always two opposing electrodes located at the same height in the longitudinal direction of the reactor shaft, forming an electrode pair, particularly an opposing electrode pair. More specifically, it is conceivable to arrange a large number of electrode pairs in the reactor. The electrodes here can have a wide variety of different geometric configurations. Thus, it is conceivable for the electrodes of an electrode pair to have a quadrangular, particularly rectangular or square, configuration. Circular, elliptical, or polygonal electrodes are also conceivable. It is also possible to use electrodes in the form of a mesh, also known as a mesh electrode. The geometry and configuration of the electrodes should not be limited to the defined shapes in the context of the present invention. However, it is advantageous if both electrodes of an electrode pair are identical to each other but have at least equivalent geometric shapes. Furthermore, it is also possible for the electrode pairs used in the reactor, particularly on the side walls of the reactor shaft, to have different shapes from each other. This can be advantageous in terms of the resulting electric field differences and the associated different heat inputs in different height regions of the reactor shaft. The use or arrangement of multiple electrode pairs in the reactor shaft advantageously allows the establishment of different axial temperature zones, and therefore advantageously allows controlled adjustment of the temperature via magnetic field parameters in the case of different resistivity properties of the particulate material of the moving bed.

[0017] Also, when viewed in the vertical longitudinal direction of the reactor, at least one of the electrodes per sidewall of the reactor shaft is at least partially positioned in the center of the reactor shaft, or each of the electrodes per sidewall is positioned at least above or below the center of the reactor shaft. More specifically, when two or more electrode pairs are positioned in the reactor shaft, at least one electrode pair is positioned in the central region of the reactor shaft (viewed in the longitudinal direction of the reactor shaft) so that at least a portion of each electrode of this electrode pair contacts the (theoretical) centerline of the reactor shaft. This may be one of the middle or outer electrode pairs. Alternatively, each electrode pair may be above or below the theoretical centerline, or the theoretical centerline may be configured such that at least one electrode pair is positioned above and below the theoretical centerline, and none of the electrode pairs, particularly the electrodes of one electrode pair, contacts this theoretical centerline.

[0018] Advantageously, the electrodes are arranged so that they generate an essentially uniform electric field, in particular a partially at least intermittently uniform electric field, when viewed in cross section, which electric field (potential field) advantageously extends horizontally over the entire width and depth (area) of the reactor shaft.

[0019] In one embodiment, the reactor has a reactor head and a reactor bottom, which may also be referred to as a reactor base. The reactor head and the reactor bottom each have at least intermittently closable feed and discharge openings, through which at least a fluid, such as a gas or a liquid, and / or solids, particularly particles, can be introduced or discharged. To generate a moving bed, the particles are continuously introduced at least intermittently into the reactor shaft through the reactor head. It is also conceivable to use a fluidized bed instead of a moving bed. The moving bed advantageously transports particles, particularly carbon-containing particles, into the reactor, particularly into the reactor shaft of the reactor, and advantageously moves / transports them through the reactor shaft, proceeding from the reactor head to the reactor bottom. Advantageously, the moving bed or bed particles move through the reactor shaft in a gravity-driven and / or gravimetric manner. The particles of the moving bed then pick up carbon in the hydrocarbon-containing fluid introduced into the reactor shaft and advantageously transport it out of the reactor shaft via the reactor bottom. In the case of pyrolysis of methane, the particles are heated, and methane decomposes preferentially on the heated particles. Some also decomposes in the intermediate volume and is discharged in the manner described. The continuous outward transport of carbon or carbon-containing particles partially ensures the maintenance of the desired electric field, which is at least intermittently uniform, and thus essentially uniform distribution of heat at least in the heating zone of the reactor shaft. The supply and discharge openings advantageously allow the continuous introduction or discharge of reactants or gases from which carbon has already been removed by pyrolysis.

[0020] It is further contemplated that the electrodes are arranged so as to generate an electric field aligned at least partially perpendicular to the direction of movement of the particles of the moving bed moving through the reactor shaft. Advantageously, due to their arrangement in the reactor shaft, i.e., due to their arrangement on two mutually opposing side walls of the reactor shaft at the same height, the electrodes generate an electric field aligned completely perpendicular to the direction of movement of the moving bed, in particular the particles of the moving bed. As described above, the moving bed moves through the reactor shaft from top to bottom, i.e., from the reactor head, where the particles of the moving bed are introduced into the reactor shaft, to the reactor bottom, which may also be called the reactor base. The particles of the moving bed then exit the reactor shaft through corresponding outlet openings. Due to the perpendicular alignment of the electric field with respect to the particles of the moving bed, uniform heating of the particles of the moving bed is advantageously achieved, so that these particles can help to capture carbon from the carbon-containing fluid across the entire cross-sectional plane of the reactor shaft. This advantageously avoids the occurrence of local hot spots.

[0021] In a second aspect of the present invention, a method for the thermal decomposition of at least a hydrocarbon-containing fluid, e.g., a gas or liquid, to produce at least a hydrogen-containing fluid, e.g., a gas or liquid, is claimed. According to the invention, the hydrocarbon-containing fluid is fed into the reactor shaft (also called the reaction space) of the reactor in countercurrent flow to a moving bed of particles. According to the invention, at least the particles of the moving bed or the hydrocarbon-containing fluid are heated to a predetermined temperature in the range of 800 to 1600°C, preferably 800 to 1500°C, and more preferably 800 to 1400°C, by electrodes for generating thermal energy arranged in the reactor shaft. More specifically, it is contemplated that either the particles of the moving bed or the hydrocarbon-containing particles, or both, i.e., the particles of the moving bed and the hydrocarbon-containing fluid, are heated (raised) by electrical energy generated by the electrodes. Advantageously, pyrolysis, i.e., dissociation of carbon and hydrogen from the hydrocarbon-containing fluid, occurs at temperatures above about 800°C. Advantageously, the electrodes generate heat in that electrical energy is dissipated into thermal energy, primarily in conjunction with the electrical resistance of the particle bed or the particles of the moving bed.

[0022] Advantageously, the process is carried out in a reactor according to the first aspect of the invention, i.e. of the type described above, and therefore the features detailed in relation to the first aspect of the invention, i.e. the reactor of the invention, are hereby incorporated by full reference.

[0023] The particles of the moving bed are considered to move gravimetrically, particularly gravity-driven, downward from the reactor head to the reactor bottom in the vertical longitudinal direction of the reactor. Thus, the particles of the moving bed are fed into the reactor shaft through one or more feed openings in the reactor head and move through the reactor shaft toward the reactor bottom. The reactor bottom preferably has one or more discharge openings through which the particles, preferably containing carbon, are withdrawn from the reactor shaft.

[0024] Advantageously, electrodes arranged in the reactor shaft, in particular on the side or inner wall of the reactor shaft, generate an electric field that is aligned at least partially, advantageously over the entire extent, perpendicular to the direction of movement of the particles of the moving bed moving through the reactor shaft. Thus, the electric field extends essentially horizontally when viewed in a cross-sectional direction, while the particles move essentially vertically through the reactor shaft when viewed in a longitudinal or longitudinal cross-sectional direction. This advantageously allows essentially complete heating of at least the particles of the moving bed at least in the heating zone of the reactor shaft, avoiding or at least counteracting the formation of local hot spots in the reactor shaft.

[0025] In one embodiment, a first heat integration zone, a reaction zone, a heating zone, and a second heat integration zone are formed in the reactor shaft. Viewed in the vertical longitudinal direction of the reactor, the individual zones, running from the reactor bottom (also called the reactor base) to the reactor head, are continuous and at least partially overlapping in parts. More specifically, overlapping zones and / or zones adjacent to each other without overlapping exist. The heating zone is primarily formed in the region of the reactor shaft where the electrodes are located. It is conceivable that the heating zone and the reaction zone at least partially overlap. This means, conversely, that the reaction, i.e., dissociation, in particular the separation of carbon from the hydrocarbon-containing fluid, is already at least partially taking place outside the heating zone, in particular in the reaction zone. The individual zones are again described in more detail below in the description of the figures.

[0026] Advantageously, the pyrolysis is carried out in at least the reaction zone or the heating zone. More specifically, it is contemplated that the pyrolysis, i.e., the decomposition of the hydrocarbon-containing fluid, in particular the gas, and thus the separation of carbon from the hydrocarbon-containing fluid, occurs in either the reaction zone or the heating zone, or in both zones. Advantageously, the pyrolysis is carried out in the overlapping region of the two zones, as described above.

[0027] It is further contemplated that the hydrocarbon-containing fluid is at least preheated in the first heat integration zone by the moving bed particles, which have already passed through the heating zone and are moving countercurrently to the hydrocarbon-containing fluid. More specifically, the hydrocarbon-containing fluid is introduced, particularly injected, into the reactor shaft through the reactor bottom (also referred to as the reactor base), particularly through at least one feed opening. Thus, the hydrocarbon-containing fluid proceeds from the reactor base and moves upward substantially vertically through the reactor shaft to the reactor head. This flow of hydrocarbon-containing particles opposes the flow of the moving bed particles, which move essentially vertically downward from the reactor head through the reactor shaft to the reactor bottom. On their path through the reactor shaft, the moving bed particles have already passed through at least a heating zone and absorbed heat / thermal energy in that heating zone before reaching the first heat integration zone. Then, when the moving bed particles encounter the hydrocarbon-containing fluid in the first heat integration zone, they release heat (thermal energy) to the hydrocarbon-containing fluid. As a result, in the first heat integration zone, the hydrocarbon-containing fluid is already preheated before reaching the heating zone. It is conceivable that the hydrocarbon-containing fluid is preheated to a temperature of 600-800 °C in the first heat integration zone. If a temperature of at least 800 °C is reached during flow through the first heat integration zone, a reaction zone is formed above this temperature, where carbon is separated from the hydrocarbon-containing fluid and deposited on the particles of the moving bed. Thus, pyrolysis of the hydrocarbon-containing fluid can already begin in the reaction zone, where it occurs due to the thermal energy provided by the particles of the moving bed. Similarly, it is conceivable that the hydrocarbon-containing fluid introduced into the reactor shaft of the reactor is already preheated before entering, so that it enters the reactor shaft in preheated form. Here, it is conceivable to preheat the hydrocarbon-containing fluid, for example, to a temperature of 600 °C or less, advantageously less than 800 °C. As a result, it is possible to accelerate the development of the reaction zone after introducing the preheated hydrocarbon-containing fluid into the reactor shaft. In particular, the preheated hydrocarbon-containing fluid can be heated to a temperature of at least 800° C. more quickly in the first heat integration zone than a non-preheated hydrocarbon-containing fluid.Due to the faster development of the reaction zone due to the attainment of a pyrolysis temperature of 800°C, pyrolysis can consequently also be carried out more quickly (compared to pyrolysis in the case of a hydrocarbon-containing fluid that is not introduced in preheated form), so that the entire pyrolysis process can be carried out in a more energy-efficient or energy-efficient manner. However, when preheating the hydrocarbon-containing fluid outside the reactor or at least outside the reactor shaft (reaction space), it is necessary to ensure that a temperature of 800°C (pyrolysis temperature) is not reached or exceeded in order to allow pyrolysis to occur in the reactor shaft.

[0028] Advantageously, the particles of the moving bed entering the reactor shaft are already at least preheated in the second heat integration zone by a heated hydrogen-containing fluid, which flows countercurrently to the particles of the moving bed and originates from the hydrocarbon-containing fluid, has already passed through the heating zone, and released carbon. Therefore, the second heat integration zone is a zone upstream of the heating zone, viewed from the reactor head to the bottom of the reactor. The hydrocarbon-containing fluid, which separates carbon at least in the reaction zone, advantageously also in the heating zone, then flows through the second heat integration zone as a hydrogen-containing fluid, which introduces corresponding heat (thermal energy) from the reaction zone and ultimately from the heating zone into the second heat integration zone. This thermal energy is then transferred to the particles of the moving bed, which are advantageously introduced into the reactor shaft in a non-preheated form. As a result, the particles of the moving bed are already preheated in the first heat integration zone by the thermal energy of the hydrogen-containing fluid before they reach the heating zone.

[0029] In one embodiment, the carbon-containing particles in the moving bed are discharged from the reactor shaft through the reactor bottom of the reactor. It is conceivable that the particles in the moving bed are sent to a downstream process that either washes the particles, i.e., removes the carbon particles, or sends the carbon-containing particles to a further chemical process for further processing. At least a portion of the particles in the moving bed grow in size due to the reactions that have taken place. The grown particles, especially the larger particles, are primarily discharged from the process, while the smaller particles, which remain unchanged in size, especially substantially unchanged, are recycled. It is further conceivable that at least a portion of the grown (large) particles are crushed and / or pulverized, especially crushed, and these crushed particles are fed back into the process.

[0030] All the advantages already described for the reactor according to the first aspect of the invention arise in the method described.

[0031] It will be clear that the features specified above and those not yet described below can be used not only in the specific combinations specified but also in other combinations or alone without departing from the scope of the invention.

[0032] Embodiments of the inventive reactor and the inventive method are explained in detail below with reference to the drawings, which respectively show, in schematic form: [Brief explanation of the drawings]

[0033] [Figure 1] FIG. 1 is a cross-sectional side view of one embodiment of the reactor of the present invention. [Figure 2] FIG. 2 is a cross-sectional top view of the embodiment of the reactor of the present invention shown in FIG. 1. [Figure 3] FIG. 2 is a cross-sectional front view of the electrode arrangement of one embodiment of the reactor of the present invention. [Figure 4] FIG. 10 is a cross-sectional front view of a further arrangement of electrodes of one embodiment of the reactor of the present invention. [Figure 5] FIG. 10 is a cross-sectional front view of a further arrangement of electrodes of one embodiment of the reactor of the present invention. [Figure 6] 1A-1C are top views of different electrode geometries. [Figure 7] FIG. 1 shows an exemplary temperature profile of one embodiment of a reactor of the present invention to illustrate the process of the present invention. DETAILED DESCRIPTION OF THE INVENTION

[0034] Elements having the same function and mode of operation are given the same reference numerals in Figures 1 to 7, respectively.

[0035] FIG. 1 shows a schematic cross-sectional side view of an embodiment of a reactor 1 of the present invention. More specifically, this is a longitudinal section of an embodiment of a reactor 1 of the present invention. FIG. 2 shows a cross-sectional top view of the embodiment of a reactor 1 of the present invention shown in FIG. 1. More specifically, FIG. 2 shows a cross-sectional view of the embodiment of a reactor 1 of the present invention shown in FIG. 1, extending essentially along the center line M shown in FIG. 1. Consequently, the reactor 1 is cut centrally, i.e., in the middle, according to FIG. 2. Therefore, FIGS. 1 and 2 will be described together below. The reactor 1 has a reactor shell 2 having a circular cross-sectional geometric shape and extending in a tower-like manner in a longitudinal direction L. The reactor shell 2 is completely closed, and consequently has a closed reactor shell wall 20 also having a circular cross-section. A reactor shaft 3 is arranged within the reactor shell 2 or the reactor shell wall 20. The reactor shaft 3 has a quadrangular, in particular square, cross-section and a tower-like geometric shape extending in a longitudinal direction L. The reactor shaft 3 thus includes at least four side walls 30, 31, 32, and 33, particularly the reactor shaft walls 30, 31, 32, and 33. At least two of the side walls 30, 31, 32, and 33, particularly the first side wall 30 and the third side wall 32, are parallel to one another. The reactor shaft 3 is thus a reaction space having a reaction volume 34 in which a chemical reaction, particularly the thermal decomposition of a hydrocarbon-containing fluid, primarily a hydrocarbon-containing gas, occurs. A reactor lining 4 is provided between the reactor shaft 3, particularly the side walls 30, 31, 32, and 33 of the reactor shaft 3, and the reactor shell 2, particularly the reactor shell wall 20. This reactor lining 4 advantageously extends completely between the reactor shaft 3 and the reactor shell 2 in the circumferential direction and the longitudinal direction L. The reactor lining 4 primarily serves to shield the reactor shell from the thermal energy introduced into the reaction volume 34 of the reactor shaft 3. 1 and 2 further show a total of six electrodes 10, 11, 12, 13, 14, 15, which are arranged on the reactor shaft 3, more particularly on the first side wall 30 and the third side wall 32 of the reactor shaft 3. Thus, three electrodes 10, 12, and 14 are arranged on the first side wall 30, and three further electrodes 11, 13, and 15 are arranged on the third side wall 32.Preferably, in a cross-sectional view, each of the electrodes 10, 11, 12, 13, 14, and 15 extends across the entire width of the side walls 30 and 32. The second side wall 31 and the fourth side wall 33 are primarily free of electrodes. The opposing electrodes 10, 11, 12, 13, 14, and 15 form electrode pairs 101, 102, and 103, respectively. For example, electrodes 10 and 11 form the first electrode pair 101, electrodes 12 and 13, the second electrode pair 102, and electrodes 14 and 15 form the third electrode pair 103. Advantageously, in a longitudinal direction L, each of the electrodes 10, 11, 12, 13, 14, and 15 of each of the electrode pairs 101, 102, and 103 is at the same height. The symbol M indicates a centerline feature. This (theoretical) centerline M therefore defines the center of the reactor 1 in the longitudinal direction L, in particular the center of the reactor shaft 3. The electrodes 10, 11, 12, 13, 14, 15 are mainly arranged, in particular in the region near the centerline M. As shown in particular in FIG. 1 , at least a first electrode pair 101 consisting of the electrodes 10 and 11 partially contacts the centerline. In contrast, a second electrode pair 102 consisting of the electrodes 12, 13 and a third electrode pair 103 consisting of the electrodes 14, 15 are shifted above the centerline M, i.e., towards the reactor head 5 of the reactor 1, in particular in the part of the reactor shaft 3 extending between the centerline M and the reactor head 5. In contrast, the part of the reactor shaft 3 extending from the centerline M towards the reactor bottom 6 does not have any further electrode pairs. The arrangement of the electrodes 10, 11, 12, 13, 14, 15 within the reactor shaft 3 with respect to the height of the reactor shaft 3 extending in the longitudinal direction L may be individually designed and is determined by the desired position of the heating zone and the resulting reaction zone. More specifically, the positioning of the electrodes 10, 11, 12, 13, 14, 15 also depends accordingly on whether the heating zone is formed in an upper or lower region of the reactor shaft 3 relative to the centerline M. This variable positioning of the electrodes 10, 11, 12, 13, 14, 15 is also shown, for example, in Figures 3, 4, and 5 below.

[0036] 3, 4 and 5 each show a cross-sectional front view of the electrode arrangement in one embodiment of the reactor 1 of the present invention.

[0037] As shown in Figure 3, the three electrode pairs 101, 102, 103 used here are arranged in the reactor shaft 3 so that the electrode of the second electrode pair 102 is at least partially in contact with the (theoretical) center line M and is therefore located at least in part in the center of the reactor shaft 3. The remaining electrode pairs 101 and 103 are then arranged in the reactor shaft 3 at a distance from the center line M. Thus, the electrode of the first electrode pair 101 is arranged in the region of the reactor shaft 3 between the center line M and the reactor bottom 6, i.e., in the region below the center line M, and the electrode of the third electrode pair 103 is arranged in the region of the reactor shaft 3 between the center line M and the reactor head 5, i.e., in the region above the center line M.

[0038] 4, an arrangement of only two electrode pairs 101 and 102 is also conceivable, in which none of the electrode pairs 101, 102, and in particular none of the electrodes of each electrode pair 101, 102, even partially contacts the theoretical centerline M. Instead, the electrode of the first electrode pair 101 is located in the region of the reactor shaft 3 between the centerline M and the reactor bottom 6, i.e., in the region below the centerline M, and the electrode of the second electrode pair 102 is located in the region of the reactor shaft 3 between the centerline M and the reactor head 5, i.e., in the region above the centerline M.

[0039] 5, a configuration with only one electrode pair 101 is also conceivable. In this case, each electrode of this electrode pair 101 at least partially contacts the (theoretical) center line M and advantageously extends across this center line M into the upper region of the reactor shaft 3 formed between the center line M and the reactor head 5, as well as into the lower region of the reactor shaft 3 formed between the center line M and the reactor bottom 6. The electrodes of the electrode pair 101 are mainly arranged so that the larger surface area of ​​each electrode of the electrode pair 101 is in the upper region of the reactor shaft 3. The electrodes of the electrode pair 101, i.e. the electrode pair 101, are therefore arranged slightly offset towards the top relative to the center line M.

[0040] Alternative positions of the electrodes per electrode pair 101, 102, 103 and alternative numbers of electrode pairs 101, 102, 103 are contemplated, meaning that more than three electrode pairs 101, 102, 103 may be arranged in the reactor shaft 3. However, more than just the number and positions of the electrode pairs 101, 102, 103 in the reactor shaft 3 may also be varied.

[0041] As shown in Figure 6, the electrodes 10, 11, 12, 13, 14, and 15 may also have different geometric configurations. For example, the use of a mesh electrode 16 or a circular electrode 17 is contemplated, as is the use of square, particularly rectangular, electrodes 18 and 19. The sizes of the electrodes 16, 17, 18, and 19 may also vary. For example, the dimensions of a rectangular large-area electrode 19 may be such that it essentially encompasses the size of at least two, particularly three or more, rectangular electrodes 18, and thus may be positioned alone or together with electrodes 19 of the same geometric shape in the reactor shaft to form an electrode pair. The use or placement of multiple electrode pairs 101, 102, and 103 in the reactor shaft 3 advantageously allows for the establishment of different axial temperature zones. Therefore, in the case of different resistivity characteristics of the particulate material in the moving bed, controlled temperature adjustment via electric field parameters is advantageously possible.

[0042] FIG. 7 shows an exemplary temperature profile of an embodiment of the reactor 1 of the present invention to illustrate the method of the present invention. The temperature profile of FIG. 7 is explained in conjunction with the basic structure of the reactor 1, as shown in FIGS. 1 and 2, for example. Temperature is plotted on the x-axis of the temperature profile. Exemplary threshold values ​​are 800°C and 1500°C. The axial extent of the reactor shaft 3 in the longitudinal direction L is shown on the y-axis. The heat generation shown in FIG. 7 occurs in the reaction volume 34 of the shaft 3 of the reactor 1 of the present invention. A hydrocarbon-containing fluid 40 is introduced into the reactor shaft 3, specifically into the reaction volume 34 of the reactor shaft 3, through an inlet / feed opening in the reactor bottom 6 (not shown), and moving bed particles 50 are introduced through an inlet / feed opening in the reactor head 5 (not shown). The hydrocarbon-containing fluid 40 flows through the reactor shaft 3, proceeding from the reactor bottom 6 toward the reactor head 5. The moving bed particles 50 move in the opposite direction, from the reactor head 5 through the reactor shaft 3 toward the reactor bottom 6. The hydrocarbon-containing fluid 40 may already be preheated before entering the reactor shaft 3. Possible temperatures are below 800°C, in particular essentially around 600°C. However, it is also conceivable that the hydrocarbon-containing fluid 40 is introduced into the reactor shaft 3 without preheating. Essentially simultaneously, the moving bed particles 50 are also introduced into the reactor shaft 3 and move through the second heat integration zone W2, the heating zone B, the reaction zone R, and the first heat integration zone W1 on their way through the reactor shaft 3 to the reactor bottom 6. In the second heat integration zone W2 formed between the heating zone B and the reactor head 5, the moving bed particles 50 are preheated in the reactor shaft 3. This is achieved by the transfer of thermal energy from the heated hydrogen-containing gas 41 coming from the heating zone B to the moving bed particles 50, which then exit the reactor shaft 3 through an outlet / discharge opening in the reactor head 5 (not shown here). As a result, in the second heat integration zone W2, an integration of heat / thermal energy from the gas phase to the solid phase takes place advantageously. Hydrogen-containing gas 41 is a reaction product formed as a result of the pyrolysis of the hydrocarbon-containing fluid 40 introduced into the reactor shaft 3.The pyrolysis advantageously takes place in the reaction zone R and at least partially in the heating zone B, advantageously also in the overlapping region of the reaction zone R and the heating zone B. To induce pyrolysis, i.e., the thermal dissociation of hydrocarbons into carbon and hydrogen components and consequently the separation of carbon from the hydrocarbon-containing fluid 40, a minimum temperature of approximately 800°C is required. This minimum temperature is advantageously already reached after passing through the first heat integration zone W1. In this first heat integration zone W1, thermal energy is transferred to the hydrocarbon-containing fluid 40 flowing in the direction of the heating zone B from the particle load 51 of the moving bed, which has already traveled through the heating zone B on its way to the reactor bottom 6. As a result, in the first heat integration stage W1, heat / thermal energy integration from the solid phase to the gas phase advantageously takes place. The closer the hydrocarbon-containing fluid 40 is to the heating zone B, the warmer it becomes due to the constant absorption of thermal energy via the particle load 51 of the moving bed. In the context of the present invention, the term "loaded particles of the moving bed 51" is understood to mean particles that have already absorbed carbon or carbon atoms from the hydrocarbon-containing fluid 40. Carbon is primarily deposited on and between the moving bed particles 50. This deposition affects the electrical resistance characteristics of the moving bed or bed of moving bed particles moving gravitationally through the reactor shaft 3. Due to the arrangement of the electrodes 10, 11, 12, 13, 14, and 15 shown by way of example in FIG. 1 within the at least rectangular reactor shaft 3, the resulting potential field, and the flow direction of the moving bed, the moving bed or bed particles 50 transfer new particle material to the heating zone B, thereby preventing the aforementioned adverse effects on the resistance characteristics. The heating zone B in the context of the present invention is understood to mean the zone in which the electrodes 10, 11, 12, 13, 14, and 15 are at least partially, advantageously completely, located or disposed. More specifically, the electrodes 10, 11, 12, 13, 14, and 15 generate the heating zone B due to their heat input. Electrodes 10, 11, 12, 13, 14, 15 advantageously do not impede the flow of particles 50 in the moving bed. Upon reaching a heating of the hydrocarbon-containing fluid of about 800° C., the resulting pyrolysis process begins and a reaction zone R is formed. This means that carbon in the hydrocarbon-containing fluid 40 moves towards the particles 50 or towards the at least partially already loaded particles 51 in the moving bed.Thus, this chemical reaction process can proceed upstream of heating zone B, i.e., before reaching the zone formed by electrodes 10, 11, 12, 13, 14, and 15, solely by heating the hydrocarbon-containing fluid 40 with the thermal energy of the moving bed particles 51. Within heating zone B, the moving bed particles 50, and thus the hydrocarbon-containing fluid 40, are heated to a maximum temperature of, advantageously, 1200°C to 1700°C. Within this heating zone B, pyrolysis proceeds until essentially all carbon has been transferred from the hydrocarbon-containing fluid 40 to the moving bed particles 50. All that remains are the hydrogen-containing fluid 41 and the moving bed particles, or at least partially loaded particles 51. Therefore, it is conceivable that the chemical reaction is already complete even before the hydrocarbon-containing fluid 40 has completely flowed through heating zone B. Therefore, it is conceivable that reaction zone R only partially overlaps heating zone B, rather than encompassing the entire length of heating zone B. [Explanation of symbols]

[0043] 1. Reactor 2. Reactor shell 3 Reactor shaft 4. Reactor Lining 5. Reactor Head 6. Bottom of reactor 10, 11, 12, 13, 14, 15 electrodes 16 mesh electrodes 17 Circular electrode 18 square / rectangular electrode 19 Square large electrode 20 Reactor shell wall 30, 31, 32, 33 Reactor shaft wall / side wall 34 reaction volumes 40 Hydrocarbon-containing fluids 41 Hydrogen-containing fluids 50 Unladen particles in moving beds 51 Particle loading on moving beds 101, 102, 103 electrode pairs B Heating Zone L Longitudinal direction M center line R Reaction Zone W1 First heat integration zone W2 Second heat integration zone x and y axes

Claims

1. A reactor (1) for the thermal decomposition of a hydrocarbon-containing fluid (40) for the production of a hydrogen-containing fluid (41), comprising: The reactor (1) has a reactor shell (2) and a reactor shaft (3) arranged in the reactor shell (2), and a reactor lining (4) for heat sealing the reactor shaft (3) to the reactor shell (2) is arranged between the reactor shell (2) and the reactor shaft (3); the reactor shell (2) of the reactor (1) has a circular cross-sectional shape, the reactor shaft (3) has a quadrilateral or polygonal shape with pentagons or more in cross-section, and at least one electrode (10, 11, 12, 13, 14, 15) for generating thermal energy is arranged on one of two mutually opposing side walls (30, 31, 32, 33) of the reactor shaft (3); A reactor (1) characterized in that

2. When viewed from the vertical longitudinal direction (L) of the reactor (1), at least portions of the electrodes (10, 11, 12, 13, 14, 15) facing each other are arranged in the center of the reactor shaft (3). characterized in that The reactor (1) according to claim 1.

3. at least two or more electrodes (10, 11, 12, 13, 14, 15) for generating thermal energy are arranged on each of the two mutually opposing side walls (30, 31, 32, 33) of the reactor shaft (3), and at least one of the electrodes (10, 11, 12, 13, 14, 15) per side wall (30, 31, 32, 33) of the reactor shaft (3) is arranged on the reactor shaft (3) as viewed in the vertical longitudinal direction (L) of the reactor (1), so that at least a portion of each of the electrodes (10, 11, 12, 13, 14, 15) is arranged in the center of the reactor shaft (3), or each of the electrodes (10, 11, 12, 13, 14, 15) per side wall (30, 31, 32, 33) is arranged above or below the center of the reactor shaft (3); characterized in that A reactor (1) according to claim 1 or 2.

4. the electrodes (10, 11, 12, 13, 14, 15) are arranged to generate an electric field that is uniform and seen across the cross section; characterized in that A reactor (1) according to any one of claims 1 to 3.

5. the reactor (1) has a reactor head (5) and a reactor bottom (6), the reactor head (5) and the reactor bottom (6) each having at least intermittently closable feed openings and discharge openings through which at least a fluid or a solid can be introduced or discharged, respectively, and solid particles (50) are continuously introduced at least intermittently through the reactor head (5) into the reactor shaft (3) to form a moving bed; characterized in that A reactor (1) according to any one of claims 1 to 4.

6. the reactor bottom (6) has at least an intermittently closable discharge opening through which at least solid particles can be discharged; characterized in that A reactor (1) according to claim 5.

7. the electrodes (10, 11, 12, 13, 14, 15) are arranged to generate an electric field aligned at least partially perpendicular to the direction of movement of the solid particles (50) of the moving bed moving through the reactor shaft (3); characterized in that A reactor (1) according to claim 5 or 6.

8. 1. A process for the thermal decomposition of a hydrocarbon-containing fluid (40) for the production of a hydrogen-containing fluid (41), wherein the hydrocarbon-containing fluid (40) is fed into a reactor shaft (3) of a reactor (1) in countercurrent to a moving bed of particles (50) therein, The method is carried out in a reactor (1) according to any one of claims 1 to 7, wherein the particles (50) of the moving bed or the hydrocarbon-containing fluid (40) are heated to a predetermined temperature in the range of 800 to 1600 °C by electrodes (10, 11, 12, 13, 14, 15) for generating thermal energy, which are arranged in the reactor shaft. A method characterized by:

9. the particles (50) of the moving bed or the hydrocarbon-containing fluid (40) are heated to a predetermined temperature in the range of 800 to 1400°C by electrodes (10, 11, 12, 13, 14, 15) for generating thermal energy, which are arranged in the reactor shaft; characterized in that The method of claim 8.

10. A method carried out in a reactor (1) according to any one of claims 5 to 7, The particles (50) of the moving bed move gravitationally downward in the vertical longitudinal direction (L) of the reactor (1) from the reactor head (5) of the reactor (1) to the reactor bottom (6) of the reactor (1), characterized in that 10. The method according to any one of claims 8 to 9.

11. the electrodes (10, 11, 12, 13, 14, 15) generate an electric field aligned at least partially perpendicular to the direction of movement of the particles (50) of the moving bed moving through the reactor shaft (3); characterized in that 11. The method according to any one of claims 8 to 10.

12. A method carried out in a reactor (1) according to any one of claims 5 to 7, a first heat integration zone (W1), a reaction zone (R), a heating zone (B) and a second heat integration zone (W2) are formed in the reactor shaft (3), the individual zones of which, viewed in the vertical longitudinal direction (L) of the reactor (1), proceed from the reactor bottom (6) of the reactor (1) to the reactor head (5) of the reactor (1), are consecutive and at least partially overlapping in some places; characterized in that 12. The method according to any one of claims 8 to 11.

13. The pyrolysis occurs at least in the reaction zone (R) or the heating zone (B); characterized in that The method of claim 12.

14. the hydrocarbon-containing fluid (40) has already passed through the heating zone (B) and has already been at least preheated in the first heat integration zone (W1) by the particles (51) of the moving bed moving countercurrently to the hydrocarbon-containing fluid (40), characterized in that 14. The method of claim 12 or 13.

15. the particles (50) of the moving bed entering the reactor shaft (3) have already been at least preheated in the second heat integration zone (W2) by a heated hydrogen-containing fluid (41) which flows countercurrently to the particles (50) of the moving bed and which originates from the hydrocarbon-containing fluid (40) and has already passed through the heating zone (B) to release carbon, characterized in that 15. The method according to any one of claims 12 to 14.

16. A method carried out in a reactor (1) according to any one of claims 5 to 7, The carbon-containing particles (51) in the moving bed are discharged from the reactor shaft (3) through the reactor bottom (6) of the reactor (1). characterized in that 16. The method according to any one of claims 8 to 15.

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