REACTOR AND PROCESS FOR THE PYROLYSIS OF HYDROCARBON-CONTAINING FLUIDS

Description

[0001] The present invention relates to a reactor at least for the pyrolysis of hydrocarbon-containing fluids, at least for the production of at least hydrogen-containing fluids, wherein the reactor has a reactor shell and a reactor shaft arranged within the reactor shell, and a reactor lining is arranged between the reactor shell and the reactor shaft, at least for thermally sealing the reactor shaft against the reactor shell. Furthermore, the invention relates to a method at least for the pyrolysis of hydrocarbon-containing fluids, at least for the production of at least hydrogen-containing fluids, wherein the hydrocarbon-containing fluids are fed to a reactor shaft of the reactor in counterflow to a moving bed of the reactor consisting of particles. STATE OF THE ART

[0002] It is fundamentally known that highly endothermic reactions, which are known to occur in the chemical industry, for example, in the splitting of petroleum fractions or the reforming of natural gas or naphtha, require temperatures, particularly in the range between 500°C and 1700°C, to enable sufficient chemical decomposition. This is due to the thermodynamic limitation of the equilibrium conversion. The thermal decomposition of hydrocarbons also requires high temperatures, particularly in the range of 800 to 1600°C. Due to thermodynamic equilibrium and reaction kinetics, such high temperatures are particularly necessary for methane pyrolysis in order to achieve sufficiently high conversion rates, advantageously of more than 50%, within a very short time.

[0003] Various solutions are known from the prior art that demonstrate the provision of high temperatures to enable a pyrolysis process. For example, US Pat. Nos. 2,389,636 and 2,600,07, as well as US Pat. Nos. 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, agglomeration, and abrasion.

[0004] Oxidative processes as a heat source are described, for example, in DE600 16 59T and US Pat. No. 3,264,210. Disadvantages of the direct use of oxidative processes include the introduction of foreign substances into the reaction zone and subsequent product contamination. There is also a risk of unintentional carbon combustion or co-combustion of the reactant stream.

[0005] US 2,799,640 and DE 1 266 273 each disclose an electrical heat source. The disadvantage here is the uneven heating of the reaction zone, which, due to instabilities in the electrical heat input, leads to inhomogeneities within the reaction chamber during pyrolysis, particularly during methane pyrolysis for the production of hydrogen and pyrolysis carbon (CH4 <-> C+2H2).

[0006] Further reactors for methane pyrolysis are known from DE 10 2019 003 982 A1, DE 10 2018 132 661 A1 and DE 10 2019 002 523 A1.

[0007] The thermal pyrolysis of methane is a highly endothermic reaction that, kinetically and thermodynamically, occurs advantageously in a temperature range of approximately 1000°C and pressures up to 40 bar. In addition to hydrogen (H2), the thermal cracking also produces pyrolysis carbon (C), which in turn represents an additional valuable product. The hydrogen and pyrolysis carbon are advantageously further processed or reused and serve as fuel or as a fuel in other drives, systems, or industries.

[0008] It is generally known that pyrolysis also involves a bed of particles, particularly carbon particles, on which the carbon-containing gas, such as methane, pyrolyzes. Electrical heat input, particularly via resistance heating, is advantageous for providing the reaction enthalpy.

[0009] When using a carbon bed, the electrical current, which is introduced into the reaction chamber, for example, via the use of electrodes or pairs of electrodes, flows over this bed and dissipates into thermal energy due to the electrical resistance of the particle bed. The electrical resistance results from the contact points between the particles of the bed and the small transfer surfaces, while the carbon particles have a high electrical conductivity. For an essentially homogeneous heat input into the heating zone of the reaction chamber, a homogeneous electrical resistance, at least in some sections, across the entire cross-sectional area of ​​the reaction chamber is required. However, as is well known, paths with deviating electrical resistance repeatedly occur, so that the electrical current flows preferentially in the areas of lower electrical resistance.As a result, increased deposition of pyrolytic carbon occurs in these areas, so that the resistance along these paths of lower resistance continues to decrease. The consequence is inhomogeneities, which lead to local hotspots, a drastic local reduction in electrical resistance, blockages, and ultimately, heating failure. Internal tests have shown that in known reactors, in particular known reactor geometries (in particular known reaction chamber geometries) and known processes for pyrolysis, for example of methane, a centrally arranged carbon formation occurs within the reaction chamber, which extends in the vertical longitudinal direction centrally along the reaction chamber, at least in sections. This carbon formation consists of coalesced carbon particles.This shows that the pyrolysis carried out did not take place across the entire cross-section of the reaction chamber, but only primarily in the center of the reaction chamber. DISCLOSURE OF THE INVENTION

[0010] The causes of the occurrence of inhomogeneities in known reaction chambers and known pyrolysis processes, and the consequent failure of the heating concept of known reactors, were investigated internally by the applicant. It was determined that a strong radial temperature profile exists due to the high ratio of the wall area of ​​the reaction chamber to the reaction volume of the reaction chamber. The higher temperature in the center of the reaction chamber leads to higher conversions, i.e., to a higher deposition of carbon on the particles of the bed and consequently to greater carbon deposition from the carbon-containing gas, such as methane. The consequence is the lower electrical resistance in this region and, consequently, a concomitant preferential current flow in the region of lower electrical resistance.

[0011] It is therefore the object of the present invention to at least partially remedy the above-described disadvantages of known reactors and pyrolysis processes. In particular, the object of the present invention is to provide a reactor and a process, at least for the pyrolysis of hydrocarbon-containing fluids, which, in a simple and cost-effective manner, enable essentially homogeneous heating of the reactor shaft across the cross-section of the reactor shaft (reaction chamber) and consequently the generation and maintenance of an at least temporarily sectionally homogeneous electric field with a corresponding at least temporarily sectionally homogeneous resistance.

[0012] The above object is achieved by a reactor at least for the pyrolysis of hydrocarbon-containing fluids with the features of claim 1 and by a method at least for the pyrolysis of hydrocarbon-containing fluids with the features according to claim 6. Further features and details of the invention emerge from the subclaims, the description and the drawings. Features and details described in connection with the reactor according to the invention naturally also apply in connection with the method according to the invention and vice versa, so that with regard to the disclosure of the individual aspects of the invention, reference is or can always be made to each other. The method according to the invention is carried out in the reactor according to the invention.

[0013] The reactor according to the invention, at least for the pyrolysis of hydrocarbon-containing fluids, at least for the production of at least hydrogen-containing fluids, has a reactor shell and a reactor shaft arranged within the reactor shell. A reactor lining is arranged between the reactor shell and the reactor shaft, at least for thermally sealing the reactor shaft against the reactor shell. According to the invention, the reactor shaft has a cross-sectional shape that is at least quadrangular, in particular rectangular, with at least one electrode for generating thermal energy being arranged on each of two opposite side walls of the reactor shaft. It is also conceivable that the reactor lining also serves for electrical insulation, so that the electrical energy generated by the electrodes is not released into the external environment of the reactor. For the purposes of the invention, fluids also include gases or liquids.Hydrocarbon-containing fluids can accordingly be, for example, methane (methane gas), natural gas, or blue gas. Within the scope of the invention, the term "hydrocarbon-containing fluids" is understood to mean all fluids (gases / liquids) that contain hydrocarbons that can be dissociated into carbon and hydrogen by means of a pyrolysis process. The reactor shell advantageously has an annular / circular geometry in cross-section. This is particularly advantageous for withstanding high pressures. However, it would also be conceivable for the reactor shell, in comparison to the reactor shaft, which can also be referred to as the reaction chamber, to also have an at least quadrangular geometry in cross-section and to be particularly advantageously adapted to the geometry of the reactor shaft. The reactor shaft can advantageously also have a rectangular, in particular square, geometry in cross-section.The reactor shaft has a cross-sectional geometry with four or more than four corners.

[0014] Particularly advantageously, at least two opposing walls, in particular inner walls of the reactor shaft, are designed to be parallel and opposite one another when viewed in cross-section through the reactor shaft. The electrodes for generating an at least temporarily sectionally homogeneous electric field, in particular a substantially homogeneous electric field, within the reactor shaft are advantageously arranged on these parallel and opposite walls. The electrodes are also advantageously arranged opposite one another, i.e., at the same height when viewed in the longitudinal direction of the reactor shaft. Particularly advantageously, the electrodes are arranged on the inside of the side walls of the reactor shaft. The arrangement of the electrodes advantageously provides direct electrical, resistive heating of the particles of the moving bed, in particular of the particle bed.The quadrangular, particularly rectangular, and particularly square geometry of the reactor shaft and the correspondingly described arrangement of the electrodes enable the generation of an at least temporarily homogeneous electric potential field between the opposing electrodes. Furthermore, this prevents the formation of slippage for the material flows and the associated reduced conversion.

[0015] It is conceivable that the particles of the moving bed have a size of 0.5 mm to 20 mm, preferably 1 mm to 10 mm. The process for pyrolysis of the carbon-containing fluid advantageously takes place at pressures of 1 bar to 50 bar, preferably 5 bar to 30 bar. Temperatures of 800°C to 1600°C, preferably 1000°C to 1400°C, are generated.

[0016] According to one embodiment, the opposing electrodes are arranged at least partially in the center of the reactor shaft, viewed in the vertical longitudinal direction of the reactor. This means that at least one section of each reactor contacts or extends to an (imaginary) center line (center of the reactor in the longitudinal direction / viewed in longitudinal section) of the reactor, while the remaining section of the respective electrode is arranged in a reactor shaft region existing below or above this imaginary center line. More precisely, it would be conceivable for the respective electrodes to be arranged in a section of the reactor shaft facing the reactor head of the reactor or in a region of the reactor shaft facing the reactor bottom (reactor bottom) of the reactor.Alternatively, however, it is also conceivable that the respective electrodes are arranged exactly in the center of the reactor shaft (viewed in the longitudinal direction / in longitudinal section). Alternatively, it is conceivable that none of the electrodes of an electrode pair is arranged, at least in part, in the center of the reactor shaft on the reactor shaft wall or side wall of the reactor shaft, viewed in the vertical longitudinal direction of the reactor. Rather, the electrodes are then arranged exclusively in a reactor shaft area on the reactor shaft wall existing below or above this imaginary center line.

[0017] According to one embodiment, at least two or more electrodes for generating thermal energy are arranged on each of the two opposite side walls of the reactor shaft. Advantageously, two of the opposing electrodes are always arranged at the same height - viewed in the longitudinal direction of the reactor shaft - so that these electrodes form an electrode pair, in particular an opposing electrode pair. More precisely, it is conceivable that a plurality of electrode pairs are arranged in the reactor. The electrodes can have a wide variety of geometric configurations. It is therefore conceivable that the electrodes of an electrode pair are quadrangular, in particular rectangular or even square. Circular, oval, elliptical, or polygonal electrodes are also conceivable. The use of electrodes in the form of a grid, also called grid electrodes, is also possible.The geometric shape and design of the electrodes should not be limited to a defined shape within the scope of the invention. However, it is advantageous if both electrodes of an electrode pair have an identical, or at least comparable, geometric shape. Furthermore, it would be possible to use electrode pairs within a reactor, in particular on the side wall of the reactor shaft, which each have a different shape. This can be advantageous with regard to the resulting different electrical fields and the associated different heat input in the various height regions of the reactor shaft. The use or arrangement of several electrode pairs within the reactor shaft advantageously enables the setting of different axial temperature zones.Accordingly, in the case of different resistance behavior of the particle material of the moving bed, it is advantageous to adjust the temperature specifically via field parameters.

[0018] Furthermore, at least one of the electrodes per side wall of the reactor shaft is arranged, at least in part, in the center of the reactor shaft, viewed in the vertical longitudinal direction of the reactor, or each of the electrodes per side wall is arranged at least above or below the center of the reactor shaft. More specifically, when two or more electrode pairs are arranged in the reactor shaft, at least one electrode pair is located in the central region of the reactor shaft such that at least a portion of each electrode of this electrode pair contacts an (imaginary) center line of the reactor shaft (viewed in the longitudinal direction of the reactor shaft). This can be a central electrode pair or one of the outer electrode pairs.Or the electrode pairs are each located above this imaginary center line or below this imaginary center line or frame this imaginary center line in such a way that at least one electrode pair is arranged above and at least one electrode pair is arranged below this imaginary center line, wherein none of the electrode pairs, in particular the electrodes of an electrode pair, contact this imaginary center line.

[0019] Advantageously, the electrodes are arranged such that, viewed in cross-section, they generate a substantially homogeneous electric field, in particular a homogeneous electric field at least temporarily in certain sections. This electric field (potential field) advantageously extends horizontally across the entire width and depth (area) of the reactor shaft.

[0020] According to one embodiment, the reactor has a reactor head and a reactor sump, which can also be referred to as the reactor bottom. The reactor head and the reactor sump each have at least temporarily closable feed openings and discharge openings through which at least fluids, such as gases or liquids, and / or solids, in particular particles, can be introduced or discharged, so that to create a moving bed, particles are at least temporarily continuously introduced into the reactor shaft through the reactor head. Instead of a moving bed, it is also conceivable to use a fluidized bed or a vortex bed. The moving bed advantageously introduces particles, in particular carbon-containing particles, into the reactor, in particular into the reactor shaft of the reactor, and advantageously moves or transports them through the reactor shaft - starting from the reactor head to the reactor sump.Advantageously, the particles of the moving bed or the bulk material migrate through the reactor shaft driven by gravity and / or gravimetrically. The particles of the moving bed then absorb the carbon from the hydrocarbon-containing fluids introduced into the reactor shaft and advantageously transport this out of the reactor shaft via the reactor sump. In the case of pyrolysis of methane, the particles heat up and methane decomposes preferentially on the heated particles. A portion will also decompose in the intermediate volume and be discharged in the manner described. The continuous removal of the carbon or the carbon-containing particles ensures that the desired, at least temporarily, sectionally homogeneous electric field is maintained and, consequently, the essentially homogeneous heat distribution, at least in the heating zone of the reactor shaft. The feed openings orThe outlet openings advantageously enable a continuous introduction or discharge of the substances to be reacted or of the gases already purified from carbon by pyrolysis.

[0021] It is further conceivable that the electrodes are arranged in such a way that they generate an electric field that is, at least in sections, oriented orthogonally to the direction of movement of the moving bed particles moving through the reactor shaft. Due to their arrangement in the reactor shaft, i.e., due to their arrangement on two opposing parallel side walls of the reactor shaft at identical heights, the electrodes advantageously generate an electric field that is entirely orthogonal to the direction of movement of the moving bed, in particular of the moving bed particles. As previously described, the moving bed moves through the reactor shaft from top to bottom, i.e., starting from the reactor head, through which the moving bed particles are introduced into the reactor shaft, to the reactor sump, which can also be referred to as the reactor bottom.The particles of the moving bed are then discharged from the reactor shaft through corresponding outlet openings. Due to the orthogonal orientation of the electric field to the particles of the moving bed, the particles are advantageously heated evenly, allowing these particles to absorb carbon from carbon-containing fluids throughout the entire plane of the reactor shaft—as viewed in the cross-sectional direction. This advantageously prevents the occurrence of local hotspots.

[0022] According to a second aspect of the invention, a method is claimed at least for the pyrolysis of hydrocarbon-containing fluids, such as gases or liquids, at least for the production of at least hydrogen-containing fluids, such as gases or liquids. According to the invention, the hydrocarbon-containing fluids are fed to a reactor shaft of a reactor, which reactor shaft can also be referred to as a reaction chamber, in counterflow to a moving bed of the reactor consisting of particles. According to the invention, at least the particles of the moving bed or the hydrocarbon-containing fluids are heated to a defined temperature in the range between 800-1600°C, preferably between 800-1500°C, particularly preferably between 800-1400°C, by means of electrodes arranged in the reactor shaft to generate thermal energy.More specifically, it is conceivable that either the particles of the moving bed or the hydrocarbon-containing particles, or both—that is, the particles of the moving bed and the hydrocarbon-containing fluids—are warmed or heated using the electrical energy generated by the electrodes. Pyrolysis, i.e., the dissociation of carbon and hydrogen from the hydrocarbon-containing fluids, advantageously occurs at temperatures above approximately 800°C. Advantageously, the electrodes generate heat, primarily in conjunction with an electrical resistance, such as the particle bed or the particles of the moving bed, by dissipating the electrical energy into thermal energy.

[0023] According to the invention, the process is carried out in a reactor according to the first aspect of the invention, i.e., of the aforementioned type. Accordingly, the features listed for the first aspect of the invention, i.e., the reactor according to the invention, are fully utilized here.

[0024] It is conceivable that the particles of the moving bed migrate gravimetrically, in particular by gravity, from a reactor head to a reactor sump in the vertical longitudinal direction of the reactor. Accordingly, the particles of the moving bed are fed into the reactor shaft via one or more feed openings within the reactor head and migrate through the reactor shaft toward the reactor sump. The reactor sump advantageously has at least one or more discharge openings through which the particles, which are advantageously now loaded with carbon, are removed from the reactor shaft.

[0025] Advantageously, the electrodes, which are arranged in the reactor shaft, in particular on a side wall or inner wall of the reactor shaft, generate an electric field which is oriented at least in sections, advantageously over its entire circumference, orthogonal to the direction of movement of the particles of the moving bed moving through the reactor shaft. Accordingly, the electric field extends essentially horizontally when viewed in the cross-sectional direction. While the particles move essentially vertically through the reactor shaft when viewed in the longitudinal direction or longitudinal section direction. This advantageously enables essentially complete heating of at least the particles of the moving bed, at least within the heating zone of the reactor shaft, and the formation of local hotspots within the reactor shaft is avoided or at least counteracted.

[0026] According to one embodiment, a first heat integration zone, a reaction zone, a heating zone, and a second heat integration zone are formed within the reactor shaft. The individual zones are formed sequentially, starting from the reactor bottom (also called the reactor bottom) of the reactor to the reactor head of the reactor, viewed in the vertical longitudinal direction of the reactor, and overlap at least partially in sections. More precisely, there are zones that overlap and / or zones that adjoin one another without overlapping. The heating zone is formed primarily in the region of the reactor shaft in which the electrodes are arranged. It is conceivable that the heating zone and the reaction zone overlap at least partially.Conversely, this means that a reaction, i.e. a dissociation, in particular the separation of carbon from the hydrocarbon-containing fluids, already takes place - at least partially - outside the heating zone, especially in the reaction zone. The individual zones are explained in more detail below - in the figure description.

[0027] Advantageously, pyrolysis takes place at least in the reaction zone or in the heating zone. More specifically, it is conceivable that pyrolysis, i.e., the decomposition of hydrocarbon-containing fluids, especially gases, and consequently the separation of carbon from the hydrocarbon-containing fluids, takes place either in the reaction zone or in the heating zone, or in both zones. Advantageously, pyrolysis takes place in an overlapping area of ​​both zones, as described above.

[0028] It is further conceivable that the hydrocarbon-containing fluids in the first heat integration zone are at least preheated by the particles of the moving bed flowing counter to the hydrocarbon-containing fluids, which have already passed through the heating zone. More precisely, the carbon-containing fluids are introduced, in particular blown in, via the reactor sump (also called the reactor bottom) into the reactor shaft, in particular via at least one feed opening. Consequently, the hydrocarbon-containing fluids move essentially vertically upwards from the reactor sump through the reactor shaft to the reactor head. This flow of hydrocarbon-containing fluids is counteracted by a flow of particles of the moving bed, which moves essentially vertically downwards from the reactor head through the reactor shaft to the reactor sump.On the way through the reactor shaft, the particles of the moving bed have already passed through at least the heating zone before reaching the first heat integration zone and have absorbed heat or thermal energy within this heating zone. When the particles of the moving bed encounter the hydrocarbon-containing fluid in the first heat integration zone, they transfer heat (thermal energy) to the hydrocarbon-containing fluid. Consequently, the hydrocarbon-containing fluid is already preheated in the first heat integration zone before it reaches the heating zone. It is conceivable that the hydrocarbon-containing fluid is preheated to a temperature between 600 and 800°C in the first heat integration zone.If a temperature of at least 800°C is reached while flowing through the first heat integration zone, the reaction zone forms at this temperature, in which the carbon is split off from the hydrocarbon-containing fluids and deposited on the particles of the moving bed. Accordingly, it is possible that the pyrolysis of the hydrocarbon-containing fluid already begins in a reaction zone, which is formed due to the thermal energy brought by the particles of the moving bed. It is also conceivable that the hydrocarbon-containing fluids introduced into the reactor shaft of the reactor are preheated before entry and thus flow into the reactor shaft preheated. In this case, it is conceivable to preheat or preheat the hydrocarbon-containing fluids to a temperature of, for example, a maximum of 600°C, advantageously to a temperature of less than 800°C.As a result, the formation of a reaction zone can be accelerated after the preheated hydrocarbon-containing fluids have been introduced into the reactor shaft. In particular, the preheated hydrocarbon-containing fluids can be heated to a temperature of at least 800°C in the first heat integration zone more quickly than non-preheated hydrocarbon-containing fluids. Based on the faster formation of the reaction zone upon reaching the pyrolysis temperature of 800°C, the pyrolysis can also take place more quickly (compared to pyrolysis with non-preheated hydrocarbon-containing fluids), so that the entire pyrolysis process can be carried out in a more energy-efficient manner.Preheating of the hydrocarbon-containing fluids outside the reactor or at least outside the reactor shaft (reaction chamber) must be ensured, however, that the temperature (pyrolysis temperature) of 800°C is not reached or even exceeded in order to enable pyrolysis to take place inside the reactor shaft.

[0029] Advantageously, the moving bed particles entering the reactor shaft are at least preheated in the second heat integration zone by a heated, hydrogen-containing fluid flowing counter to the moving bed particles, resulting from the hydrocarbon-containing fluids, which has already passed through the heating zone and released carbon. The second heat integration zone is therefore a zone located upstream of the heating zone, viewed from the reactor head toward the reactor bottom. The hydrocarbon-containing fluids, which release carbon at least in the reaction zone and advantageously also in the heating zone, then flow through the second heat integration zone as hydrogen-containing fluids, which bring corresponding heat (thermal energy) from the reaction zone and ultimately also 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 without preheating. Consequently, the particles of the moving bed are already preheated by the thermal energy of the hydrogen-containing fluids in the first heat integration zone before they reach the heating zone.

[0030] In one embodiment, the carbon-laden particles of the moving bed are discharged from the reactor shaft via the reactor sump. It is conceivable that the particles of the moving bed are fed to subsequent processes through which the particles are purified, i.e., the carbon is removed from the particles, or through which the carbon-laden particles are fed to further chemical processes for further processing. At least some of the particles of the moving bed grow in size due to the reaction that has taken place. The grown particles, especially the large ones, are primarily discharged from the process, while the unchanged, especially the almost unchanged small particles are recirculated.It is further conceivable that at least some of the grown (large) particles are broken and / or ground, in particular crushed, whereby these crushed particles are returned to the process.

[0031] The described method provides all the advantages that have already been described for a reactor according to the first aspect of the invention.

[0032] It is understood that the features mentioned above and those to be explained below can be used not only in the combination specified in each case, but also in other combinations or on their own, without departing from the scope of the present invention.

[0033] Embodiments of the reactor according to the invention and of the process according to the invention are explained in more detail below with reference to drawings. They show schematically: Figure 1 shows a sectional side view of an embodiment of the reactor according to the invention, Figure 2 shows a sectional plan view of the reactor shown in the Figure 1 shown embodiment of the reactor according to the invention, Figure 3 in a sectional view of an arrangement of electrodes of an embodiment of the reactor according to the invention, Figure 4 in a sectional view of a further arrangement of electrodes of an embodiment of the reactor according to the invention, Figure 5 in a sectional view of a further arrangement of electrodes of an embodiment of the reactor according to the invention, Figure 6 a plan view of different geometries of electrodes, and Figure 7 an exemplary temperature profile of an embodiment of the reactor according to the invention to illustrate the process according to the invention.

[0034] Elements with the same function and mode of action are listed in the Fig. 1 to 7each provided with the same reference symbols.

[0035] In the Figure 1 is a schematic sectional side view of an embodiment of a reactor 1 according to the invention. More precisely, this is a longitudinal section through an embodiment of the reactor 1 according to the invention. Figure 2 is a sectional view of a plan view of the Figure 1 shown embodiment of the reactor 1 according to the invention. More precisely, in the Figure 2 a cross-section of the Figure 1 shown embodiment of the reactor 1 according to the invention, which extends essentially along the Figure 1 shown center line M. The reactor 1 is therefore according to the Figure 2 middle, which means cut in the middle. Therefore, the Figures 1 and 2described together below. The reactor 1 has a reactor shell 2 which has a circular geometric shape in cross section and extends like a tower in the longitudinal direction L. The reactor shell 2 is completely closed and consequently has a closed reactor shell wall 20 with 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, geometric shape in cross section and extends like a tower in the longitudinal direction L. Consequently, the reactor shaft 3 comprises at least four side walls 30, 31, 32, 33, in particular reactor shaft walls 30, 31, 32, 33. At least two of the side walls 30, 31, 32, 33, in particular the first side wall 30 and the third side wall 32, lie parallel to one another.The reactor shaft 3 is a reaction chamber which consequently has a reaction volume 34 within which the chemical reaction, in particular the pyrolysis of hydrocarbon-containing fluids, primarily hydrocarbon-containing gases, takes place. A reactor lining 4 is provided between the reactor shaft 3, in particular the side walls 30, 31, 32, 33 of the reactor shaft 3, and the reactor shell 2, in particular 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 in the longitudinal direction L. The reactor lining 4 primarily serves to shield thermal energy, which is introduced into the reaction volume 34 of the reactor shaft 3, from the reactor shell. Furthermore, the . Figures 1 and 2A total of six electrodes 10, 11, 12, 13, 14, 15 are shown, which are arranged on the reactor shaft 3, more precisely on the first side wall 30 and on the third side wall 32 of the reactor shaft 3. Accordingly, three electrodes 10, 12, and 14 are arranged on the first side wall 30, while three further electrodes 11, 13, and 15 are arranged on the third side wall 32. Advantageously, the respective electrodes 10, 11, 12, 13, 14, 15 extend, viewed in the cross-sectional direction, along the entire width of the side walls 30, 32. The second side wall 31 and the fourth side wall 33 primarily have no electrodes. Opposing electrodes 10, 11, 12, 13, 14, and 15 form an electrode pair 101, 102, and 103. Thus, electrodes 10 and 11 form the first electrode pair 101, electrodes 12 and 13 form the second electrode pair 102, and electrodes 14 and 15 form the third electrode pair 103.Advantageously, the respective electrodes 10, 11, 12, 13, 14, 15 of an electrode pair 101, 102, 103 are at the same height when viewed in the longitudinal direction L. The reference symbol M denotes the feature of the center line. This (imaginary) center line M consequently defines the center of the reactor 1, in particular of the reactor shaft 3, when viewed in the longitudinal direction L. The electrodes 10, 11, 12, 13, 14, 15 are arranged primarily in the region, more precisely in the vicinity of the center line M. As can be seen in particular in FIG. Figure 1As shown, at least the first electrode pair 101 consisting of the electrodes 10 and 11 contacts the center line in sections. The second electrode pair 102 consisting of the electrodes 12, 13 and the third electrode pair 103 consisting of the electrodes 14, 15 are, in contrast, arranged above the center line M, i.e., in the direction of the reactor head 5 of the reactor 1, in particular in a section of the reactor shaft 3 extending between the center line M and the reactor head 5. The section of the reactor shaft 3 extending from the center line M in the direction of the reactor sump 6, in contrast, has no 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 can be individually designed and is determined by the desired position of the heating zone and the resulting reaction zone.More precisely, depending on whether the heating zone is to be formed in an upper or lower area of ​​the reactor shaft 3 relative to the center line M, the electrodes 10, 11, 12, 13, 14, 15 are placed accordingly. This variable placement of the electrodes 10, 11, 12, 13, 14, 15 is also shown, for example, in the following . Figures 3, 4 and 5 .

[0036] In the Figures 3, 4 and 5 are shown in a sectional view a view of an arrangement of electrodes of an embodiment of the reactor 1 according to the invention.

[0037] As in the Figure 3As shown, the three electrode pairs 101, 102, 103 used here are positioned within the reactor shaft 3 in such a way that the electrodes of the second electrode pair 102 contact the (imaginary) center line M at least in sections and are therefore arranged in at least one section in the middle of the reactor shaft 3. The remaining electrode pairs 101 and 103 are then arranged at a distance from the center line M within the reactor shaft 3. Thus, the electrodes of the first electrode pair 101 are arranged in a region of the reactor shaft 3 between the center line M and the reactor sump 6, i.e. in a lower region of the reactor shaft 3 relative to the center line M, while the electrodes of the third electrode pair 103 are arranged in a region of the reactor shaft 3 between the center line M and the reactor head 5, i.e. in an upper region of the reactor shaft 3 relative to the center line M.

[0038] As in the Figure 4As shown, the arrangement of only two electrode pairs 101 and 102 is also conceivable, wherein none of the electrode pairs 101, 102, in particular none of the electrodes of the respective electrode pair 101, 102, contacts the imaginary center line M even in part. Rather, the electrodes of the first electrode pair 101 are arranged in a region of the reactor shaft 3 between the center line M and the reactor sump 6, i.e. in a lower region of the reactor shaft 3 relative to the center line M, while the electrodes of the second electrode pair 102 are arranged in a region of the reactor shaft 3 between the center line M and the reactor head 5, i.e. in an upper region of the reactor shaft 3 relative to the center line M.

[0039] The design using only one pair of electrodes 101 is also possible, as in the Figure 5shown, is conceivable. In this case, the respective electrodes of this electrode pair 101 contact the (imaginary) center line M at least in sections and advantageously extend beyond this center line M into the upper region of the reactor shaft 3, which is formed between the center line M and the reactor head 5, as well as into the lower region of the reactor shaft 3, which is formed between the center line M and the reactor sump 6. Primarily, the electrodes of the electrode pair 101 are arranged such that a larger area of ​​the respective electrode of the electrode pair 101 is located 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 upwards relative to the center line M.

[0040] Alternative placements of the electrodes per electrode pair 101, 102, 103, as well as an alternative number of electrode pairs 101, 102, 103, are conceivable. This means that more than three electrode pairs 101, 102, 103 can be arranged within a reactor shaft 3. However, not only the number and placement of the electrode pairs 101, 102, 103 within a reactor shaft 3 can vary.

[0041] As in the Figure 6As shown, the electrodes 10, 11, 12, 13, 14, 15 can also have different geometric designs. For example, the use of grid electrodes 16 or circular electrodes 17 is just as conceivable as the use of square, in particular rectangular, electrodes 18, 19. The size of the electrodes 16, 17, 18, 19 can also vary. For example, the rectangular, large-area electrode 19 is dimensioned such that it essentially comprises the size of at least two, in particular three or more other rectangular electrodes 18 and can therefore also be arranged alone or with a geometrically identically designed electrode 19 to create an electrode pair in the reactor shaft. The use or arrangement of several electrode pairs 101, 102, 103 within the reactor shaft 3 advantageously enables the setting of different axial temperature zones.Accordingly, in the case of different resistance behavior of the particle material of the moving bed, it is advantageous to adjust the temperature specifically via field parameters.

[0042] In the Figure 7 An exemplary temperature profile of an embodiment of the reactor 1 according to the invention is shown to illustrate the process according to the invention. The temperature profile of the Figure 7 is used in conjunction with the basic structure of reactor 1, as shown for example in the Figures 1 and 2 shown, explained. The temperature is plotted along the x-axis of the temperature profile. 800°C and 1500°C are given as examples. The axial extent of the reactor shaft 3 in the longitudinal direction L is shown along the y-axis. Figure 7The thermal development shown takes place in the reaction volume 34 of the reactor shaft 3 of a reactor 1 according to the invention. Hydrocarbon-containing fluids 40 are introduced into the reactor shaft 3, in particular into the reaction volume 34 of the reactor shaft 3, via inlet openings / feed openings not shown here in the reactor sump 6, and particles 50 of the moving bed are introduced into the reactor shaft 3, in particular into the reaction volume 34 of the reactor shaft 3, via inlet openings / feed openings not shown here in the reactor head 5 of the reactor 1. The hydrocarbon-containing fluids 40 flow from the reactor sump 6 in the direction of the reactor head 5 through the reactor shaft 3. In contrast, the particles 50 of the moving bed migrate from the reactor head 5 in the direction of the reactor sump 6 through the reactor shaft 3. The hydrocarbon-containing fluids 40 can already be preheated before entering the reactor shaft 3. Temperatures below 800°C, especially around 600°C, are suitable.However, it is also conceivable that the hydrocarbon-containing fluids 40 are introduced into the reactor shaft 3 without preheating. Essentially at the same time, the particles 50 of the moving bed are also introduced into the reactor shaft 3 and, on their way through the reactor shaft 3 to the reactor sump 6, pass through the second heat integration zone W2, the heating zone B, the reaction zone R, and the first heat integration zone W1. In the second heat integration zone W2, which forms between the heating zone B and the reactor head 5, the particles 50 of the moving bed are preheated or preheated within the reactor shaft 3. This occurs through a transfer of thermal energy, which is transferred from heated hydrogen-containing gases 41, which leave the reactor shaft 3 from the heating zone B via outlet openings / discharge openings (not shown here) within the reactor head 5, to the particles 50 of the moving bed.In the second heat integration zone W2, an integration of heat / thermal energy from the gas phase to the solid phase advantageously takes place. The hydrogen-containing gases 41 are a reaction product resulting from the pyrolysis of the hydrocarbon-containing fluids 40 introduced into the reactor shaft 3. The pyrolysis advantageously takes place in the reaction zone R and at least partially also in the heating zone B, advantageously (also) in the region of the overlap between reaction zone R and heating zone B. To trigger pyrolysis, i.e. the thermal dissociation of hydrocarbons into the components carbon and hydrogen and consequently the separation of carbon from the hydrocarbon-containing fluids 40, a minimum temperature of approximately 800°C is required. This minimum temperature is advantageously already reached after passing through a first heat integration zone W1.In this first heat integration zone W1, heat energy is transferred from the loaded particles 51 of the moving bed, which have already passed through heating zone B on their way to the reactor sump 6, to the hydrocarbon-containing fluids 40 flowing toward heating zone B. Consequently, in the first heat integration stage W1, heat / heat energy is advantageously integrated from the solid phase to the gas phase. The closer the hydrocarbon-containing fluids 40 approach heating zone B, the warmer they become due to the continuous absorption of heat energy by the loaded particles 51 of the moving bed. For the purposes of this invention, loaded particles 51 of the moving bed are particles that have already absorbed carbon or carbon atoms from the hydrocarbon-containing fluids 40. The carbons are deposited primarily on and between the particles 50 of the moving bed.This deposition influences the electrical resistance behavior of the moving bed or the packing of the moving bed, which moves gravimetrically through the reactor shaft 3. By the example shown in the . Figure 1Due to the arrangement of the electrodes 10, 11, 12, 13, 14, 15 shown within an at least rectangular reactor shaft 3 and the resulting electric potential field as well as the flow direction of the moving bed, the moving bed or the particles 50 of the moving bed pushes new particulate material into the heating zone B and thus prevents a negative influence on the aforementioned resistance behavior. The heating zone B is to be understood within the scope of the invention as a zone within which the electrodes 10, 11, 12, 13, 14, 15 are positioned or arranged at least in sections, advantageously completely. More precisely, the electrodes 10, 11, 12, 13, 14, 15 create the heating zone B due to their heat input. Advantageously, the electrodes 10, 11, 12, 13, 14, 15 do not impede the flow of the particles 50 of the moving bed. When the hydrocarbon-containing fluids reach a temperature of approx.At 800°C, the pyrolysis process begins, and reaction zone R forms. This means that the carbons of the hydrocarbon-containing fluids 40 migrate toward the particles 50 or the at least partially already loaded particles 51 of the moving bed. This chemical reaction process can therefore also occur before heating zone B and thus before reaching the zone formed by the electrodes 10, 11, 12, 13, 14, 15, solely by heating the hydrocarbon-containing fluids 40 by the thermal energy of the loaded particles 51 of the moving bed. Within heating zone B, the particles 50 of the moving bed, and consequently also the hydrocarbon-containing fluids 40, are heated to a maximum temperature of advantageously 1200°C to 1700°C.Within this heating zone B, pyrolysis continues until essentially all of the carbon from the hydrocarbon-containing fluids 40 has been transferred to the particles 50 of the moving bed. What remains are the hydrogen-containing fluids 41 and the loaded or at least partially loaded particles 51 of the moving bed. Accordingly, it is also conceivable that the chemical reaction has already been completed, even though the hydrocarbon-containing fluids 40 have not yet completely flowed through the heating zone B. Accordingly, it is conceivable that the reaction zone R does not additionally encompass the entire length of the heating zone B, but only partially overlaps it. List of reference symbols

[0043] 1Reactor 2Reactor shell 3Reactor shaft 4Reactor lining 5Reactor head 6Reactor sump 10, 11, 12, 13, 14, 15 Electrodes 16 Grid electrode 17 Circular electrode 18 Square / rectangular electrode 19 Large square electrode 20 Reactor shell wall 30, 31, 32, 33Reactor shaft walls / side walls 34Reaction volume 40hydrocarbon-containing fluid 41hydrogen-containing fluid 50unoccupied particles of the moving bed 51occupied particles of the moving bed 101,102,103Electrode pair BBeating zone LLongitudinal direction MCenter line RReaction zone W1first heat integration zone W2second heat integration zone x, y axes

Claims

1. A reactor (1) at least for pyrolysis of hydrocarbon-containing fluids (40) at least for production of at least hydrogen-containing fluids (41), wherein the reactor (1) has a reactor shell (2) and a reactor shaft (3) disposed within the reactor shell (2), and a reactor lining (4) at least for thermal sealing of the reactor shaft (3) with respect to the reactor shell (2) is disposed between the reactor shell (2) and the reactor shaft (3), characterized in that the reactor shaft (3) has a geometry with four or more than four vertices in cross section, where at least one electrode (10, 11, 12, 13, 14, 15) for generation of thermal energy is disposed on each of two mutually opposite side walls (30, 31, 32, 33) of the reactor shaft (3).

2. The reactor (1) as claimed in claim 1, characterized in that the mutually opposite electrodes (10, 11, 12, 13, 14, 15), viewed in vertical longitudinal direction (L) of the reactor (1), are disposed in the middle of the reactor shaft (3) at least in sections.

3. The reactor (1) as claimed in either of the preceding claims, characterized in that there are at least two or more electrodes (10, 11, 12, 13, 14, 15) for generation of thermal energy disposed on each of the two mutually opposite side walls (30, 31, 32, 33) of the reactor shaft (3), where at least one of the electrodes (10, 11, 12, 13, 14, 15) per side wall (30, 31, 32, 33) of the reactor shaft (3), viewed in vertical longitudinal direction (L) of the reactor (1), is disposed in the middle of the reactor shaft (3) at least in sections, or each of the electrodes (10, 11, 12, 13, 14, 15) per side wall (30, 31, 32, 33) is disposed at least above or below the middle of the reactor shaft (3).

4. The reactor (1) as claimed in any of the preceding claims, characterized in that the reactor (1) has a reactor head (5) and a reactor bottom (6), where the reactor head (5) and the reactor bottom (6) each have at least intermittently closable feed openings and discharge openings through which at least fluids or solids, especially particles, can be introduced or discharged, such that, for creation of a moving bed, particles (50) are continuously introduced into the reactor shaft (3) at least intermittently through the reactor head (5).

5. The reactor (1) as claimed in claim 4, characterized in that the electrodes (10, 11, 12, 13, 14, 15) are arranged in such a way that they generate an electrical field aligned orthogonally at least in sections to the direction of movement of the particles (50) of the moving bed that move through the reactor shaft (3).

6. A method at least for pyrolysis of hydrocarbon-containing fluids (40) at least for production of at least hydrogen-containing fluids (41), wherein the hydrocarbon-containing fluids (40) are fed to a reactor shaft (3) of a reactor (1) in countercurrent to a moving bed of the reactor that consists of particles (50), wherein at least the particles (50) of the moving bed or the hydrocarbon-containing fluids (40), by means of electrodes (10, 11, 12, 13, 14, 15) for generation of thermal energy that are disposed in the reactor shaft, are heated up to a defined temperature in the range between 800-1600°C, preferably between 800-1400°C, characterized in that the method is conducted in a reactor (1) as claimed in any of the preceding claims 1 to 5.

7. The method as claimed in claim 6, characterized in that the particles (50) of the moving bed migrate downward gravimetrically from a reactor head (5) of the reactor (1) to a reactor bottom (6) of the reactor (1) in vertical longitudinal direction (L) of the reactor (1).

8. The method as claimed in claim 6 or 7, characterized in that the electrodes (10, 11, 12, 13, 14, 15) generate an electrical field aligned orthogonally at least in sections to the direction of movement of the particles (50) of the moving bed that move through the reactor shaft (3).

9. The method as claimed in any one of claims 6 to 8, characterized in that a first heat integration zone (W1), a reaction zone (R), a heating zone (B) and a second heat integration zone (W2) are formed within the reactor shaft (3), where the individual zones, proceeding from the reactor bottom (6) of the reactor (1) to the reactor head (5) of the reactor (1), viewed in vertical longitudinal direction (L) of the reactor (1) are successive and at least partly overlap in sections.

10. The method as claimed in claim 9, characterized in that the pyrolysis takes place at least in the reaction zone (R) or in the heating zone (B).

11. The method as claimed in either of claims 9 and 10, characterized in that the hydrocarbon-containing fluids (40) are already at least preheated in the first heat integration zone (W1) by the particles (51) of the moving bed which have already passed through the heating zone (B) and move in countercurrent to the hydrocarbon-containing fluids (40).

12. The method as claimed in any of claims 9 to 11, characterized in that the particles (50) of the moving bed that enter the reactor shaft (3) are already at least preheated in the second heat integration zone (W2) by a heated hydrogen-containing fluid (41) which flows in countercurrent to the particles (50) of the moving bed, results from the hydrocarbon-containing fluids (40) and has already passed through the heating zone (B) and released carbon.

13. The method as claimed in any one of claims 6 to 12, characterized in that the carbon-laden particles (51) in the moving bed are discharged from the reactor shaft (3) via the reactor bottom (6) of the reactor (1).