Reactor and method for pyrolyzing a hydrocarbon-containing fluid

Abstract

The invention relates to a reactor and a method for at least pyrolyzing a hydrocarbon-containing fluid to produce at least a hydrogen-containing fluid, wherein the reactor has a reactor housing and a reactor shaft arranged within the reactor housing, and at least a reactor lining for thermally sealing the reactor shaft relative to the reactor housing is arranged between the reactor housing and the reactor shaft, and wherein the reactor shaft has a geometry of at least a quadrilateral in cross section, wherein at least one electrode for generating thermal energy is arranged on each of two mutually opposite side walls of the reactor shaft.

Description

Technical Field

[0001] This invention relates to a reactor and method for at least pyrolyzing a hydrocarbon-containing fluid to at least produce a hydrogen-containing fluid, wherein the reactor has a reactor shell and a reactor shaft disposed within the reactor shell, and a reactor liner for at least thermally sealing the reactor shaft relative to the reactor shell is provided between the reactor shell and the reactor shaft. The invention also relates to a method for at least pyrolyzing a hydrocarbon-containing fluid to at least produce a hydrogen-containing fluid, wherein the hydrocarbon-containing fluid is countercurrently fed into the reactor shaft of the reactor along with a moving bed of particles. Background Technology

[0002] The fundamental knowledge is that highly endothermic reactions occurring in the chemical industry (such as the cracking of mineral oil fractions or the reforming of natural gas or naphtha) require temperatures, particularly in the range of 500°C to 1700°C, to achieve sufficient chemical decomposition. This is due to the thermodynamic limitations of equilibrium conversion. The thermal decomposition of hydrocarbons also requires high temperatures, especially in the range of 800 to 1600°C. In particular, the pyrolysis of methane requires such high temperatures due to thermodynamic equilibrium and reaction kinetics to achieve sufficiently high conversion rates, advantageously greater than 50%, within a very short time.

[0003] Existing technologies disclose various solutions that demonstrate the provision of high temperatures to achieve pyrolysis methods. For example, documents US2,389,636 and US2,600,07, and US 5,486,216 and US 6,670,058 describe the use of solid beds as the heat transfer medium. However, it should be noted that this can lead to unfavorable surface effects in the range of adhesion, agglomeration, and abrasion.

[0004] For example, oxidation methods using a heat source are described in DE600 16 59T or US 3,264,210. A disadvantage of directly using oxidation methods is, for example, the introduction of foreign substances into the reaction zone, thus contaminating the products. There is also a risk that carbon will be burned off undesirably or that the reaction stream will also be combusted.

[0005] US2,799,640 or DE 1,266,273 each discloses an electrothermal source. One drawback here is considered to be the non-uniform heating of the reaction zone; this instability of the electrothermal input leads to non-uniformity in the reaction space during pyrolysis, particularly in the pyrolysis of methane used to produce hydrogen and pyrolytic carbon (CH4<->C+2H2).

[0006] The pyrolysis of methane is a highly endothermic reaction that occurs kinetically and thermodynamically favorablely over a temperature range of approximately 1000°C and pressures up to 40 bar. In addition to hydrogen (H2), the pyrolysis also produces pyrolytic carbon (C), a valuable byproduct. Both hydrogen and pyrolytic carbon can be advantageously further processed or utilized, serving as fuels for transportation or as combustion fuels in other drive systems, plants, or industrial sectors.

[0007] Particle beds, especially carbon particle beds, are also used for pyrolysis, and the pyrolysis of carbon-containing gases, such as methane, on them can be considered fundamental knowledge. In particular, the electrical input of heat via resistance heating is advantageously suited to providing the enthalpy of reaction.

[0008] When using a carbon bed, for example, current introduced into the reaction space via electrodes or electrode pairs flows through the bed and dissipates as heat due to the resistance of the particle bed. The resistance is generated by the contact points between the bed particles and low-transfer regions, while the carbon particles have high conductivity. A substantially uniform input of heat into the heating zone of the reaction space requires resistance, which is partially, at least intermittently, uniform across the entire cross-sectional area of ​​the reaction space. However, it is known that paths with varying resistances will always emerge, causing current to preferentially flow in regions of lower resistance. As a result, increased deposition of pyrolytic carbon occurs in these regions, further reducing the resistance along these lower-resistance paths. This results in non-uniformity leading to localized hot spots, localized sharp decreases in resistance, blockage, and ultimately, heating failure. Internal studies have shown that known reactors, particularly known reactor geometries (especially known reaction space geometries), and known methods of pyrolysis, such as methane, result in carbon formations centrally arranged within the reaction space, extending at least partially along the vertical longitudinal direction. These carbon formations consist of aggregated carbon particles. This indicates that the pyrolysis does not occur across the entire cross-section of the reaction space, but rather primarily occurs at the center of the reaction region.

[0009] The inhomogeneities observed in known reaction spaces and known pyrolysis methods, and consequently the reasons for the failure of known reactor heating approaches, have been the subject of this applicant's internal research. It has been found that a significant radial temperature profile exists due to the high ratio of the wall area to the reaction volume of the reaction space. The higher temperature in the middle of the reaction space leads to higher conversion rates, i.e., a higher degree of carbon deposition on the particles in the bed, and thus more carbon deposition from carbon-containing gases such as methane. As a result, the resistivity is lower in this region, and therefore, the associated current flows preferentially in regions of lower resistivity. Summary of the Invention

[0010] Therefore, the object of the present invention is to at least partially overcome the aforementioned disadvantages of known reactors and pyrolysis methods. In particular, one object of the present invention is to provide at least a reactor and method for pyrolyzing hydrocarbon-containing fluids, which enables the reactor shaft (reaction space) to be heated substantially uniformly across its cross-section in a simple and cost-effective manner, thereby generating and maintaining an electric field that is partially at least intermittently uniform and partially has a correspondingly at least intermittently uniform resistance.

[0011] The aforementioned objectives are achieved by the reactor of the present invention for at least the pyrolysis of hydrocarbon-containing fluids and by the method of the present invention for at least the pyrolysis of hydrocarbon-containing fluids. Other features and details of the invention will be apparent from the specification and drawings. The features and details described in conjunction with the reactor of the invention can of course also be applied to the method of the invention, and vice versa in each case, such that disclosure relating to various aspects of the invention is always referred to, or may be referred to, alternative subject matter. Furthermore, the method of the invention can be carried out by the reactor of the present invention.

[0012] The reactor of the present invention, used at least for pyrolyzing a hydrocarbon-containing fluid to produce at least a hydrogen-containing fluid, has a reactor shell and a reactor shaft disposed within the reactor shell. A reactor liner is provided between the reactor shell and the reactor shaft for at least thermally sealing the reactor shaft relative to the reactor shell. According to the invention, the reactor shaft has a cross-section with at least a quadrilateral geometry, wherein at least one electrode for generating heat energy is disposed on each of two opposing sidewalls of the reactor shaft. It is also conceivable that the reactor liner also serves as electrical insulation, such that the electrical energy generated by the electrodes is not released into the external environment of the reactor. In the context of the invention, fluid is also understood to mean gas or liquid. Thus, a hydrocarbon-containing fluid can be, for example, methane (methane gas), natural gas, or blue coal gas. Therefore, in the context of the invention, the term "hydrocarbon-containing fluid" should be understood to mean all fluids (gas / liquid) containing hydrocarbons that can be dissociated into carbon and hydrogen by pyrolysis. The reactor shell of the reactor advantageously has an annular / circular cross-sectional geometry. This is advantageous, particularly for withstanding high pressures. However, similarly to a reactor shaft, which can also be called a reaction space, it is conceivable that the reactor shell also has a geometry with at least a quadrilateral cross-section, and particularly advantageously, a geometry that matches the geometry of the reactor shaft. The reactor shaft can also advantageously have a rectangular cross-section geometry, particularly a square geometry. However, it is also conceivable that the reactor shaft has a polygonal, particularly a pentagonal or more-sided polygonal cross-section. Particularly advantageously, when viewed along the cross-section of the reactor shaft, there are at least two opposing walls, particularly the inner walls, which are parallel and opposite to each other. Electrodes are arranged on these parallel and opposing walls within the reactor shaft, the electrodes being used to generate a partially, at least intermittently, uniform electric field, particularly a substantially uniform electric field. Advantageously, the electrodes are also opposite to each other, i.e., at the same height when viewed in the longitudinal direction of the reactor shaft. Particularly advantageously, the electrodes are arranged on the inner side of the sidewalls of the reactor shaft. This arrangement of electrodes advantageously provides direct resistance heating of the particles in the moving bed, particularly the particle bed. The quadrilateral, especially rectangular, and especially square geometry of the reactor shaft, and the corresponding electrode arrangement, are designed to generate a partially uniform potential field, at least intermittently, between the opposing electrodes. Furthermore, this prevents any slippage in the material flow and the associated reduction in conversion.

[0013] It is conceivable that the particles in the moving bed have a size of 0.5 mm to 20 mm, preferably 1 mm to 10 mm. The pyrolysis of the hydrocarbon-containing fluid is advantageously carried out at pressures of 1 bar to 50 bar, preferably 5 bar to 30 bar. The temperatures generated here are primarily 800°C to 1600°C, preferably 1000°C to 1400°C.

[0014] In one embodiment, viewed in the vertical longitudinal direction of the reactor, the electrodes opposite each other are at least partially disposed in the middle of the reactor shaft. This means that at least a portion of each reactor is in contact with or extends upwards along the (theoretical) centerline of the reactor (the midpoint of the reactor viewed in the longitudinal direction / in the longitudinal section), while the corresponding electrodes of the remaining portions are disposed in a region of the reactor shaft existing below or above this theoretical centerline. More specifically, it is conceivable to place the corresponding electrodes in the portion of the reactor shaft facing the top of the reactor or in the region of the reactor shaft facing the bottom (base) of the reactor. However, alternatively, it is conceivable that the corresponding electrodes are precisely disposed in the middle of the reactor shaft (viewed in the longitudinal direction / in the longitudinal section). Alternatively, it is conceivable that, viewed in the vertical longitudinal direction of the reactor, neither electrode of the electrode pair is at least partially disposed in the middle of the reactor shaft wall or sidewall of the reactor shaft. Instead, the electrodes are disposed only in a region of the reactor shaft existing below or above the theoretical centerline at the reactor shaft wall.

[0015] In one embodiment, at least two or more electrodes for generating heat energy are disposed on each of two opposing sidewalls of the reactor shaft. Advantageously, two opposing electrodes are always disposed at the same height – viewed longitudinally in the reactor shaft – such that these electrodes form an electrode pair, particularly an opposing electrode pair. More specifically, it is conceivable to arrange multiple electrode pairs in the reactor. The electrodes here can have a variety of different geometries. Thus, it is conceivable that the electrodes of an electrode pair have a quadrilateral, particularly rectangular or square, construction. Similarly, circular, oval / elliptical, or polygonal electrodes are conceivable. Mesh-like electrodes, also known as mesh electrodes, can also be used. In the context of the invention, the geometry and construction of the electrodes are not limited to the defined shapes. However, it is advantageous when the two electrodes of an electrode pair have the same, or at least equivalent, geometry. Additionally, it is possible if the electrode pairs used within the reactor, particularly on the sidewalls of the reactor shaft, each have different shapes. This can be advantageous considering the differences in electric field and associated heat inputs generated in different height regions of the reactor shaft. Using or arranging multiple electrode pairs within the reactor shaft advantageously enables the establishment of different axial temperature zones. Therefore, advantageously, the temperature can be controlled by field parameters depending on the different resistance characteristics of the particulate material in the moving bed.

[0016] Furthermore, at least one electrode (viewed in the vertical longitudinal direction of the reactor shaft) on each sidewall of the reactor shaft is at least partially disposed in the middle of the reactor shaft, or each electrode on each sidewall is at least disposed above or below the middle of the reactor shaft. More specifically, in the case of two or more electrode pairs arranged in the reactor shaft, at least one electrode pair is disposed in the middle region of the reactor shaft such that at least a portion of each electrode in the electrode pair is in contact with the (theoretical) centerline of the reactor shaft (viewed in the longitudinal direction of the reactor shaft). This can be either an intermediate electrode pair or an outer electrode pair. Alternatively, each electrode pair is either above or below the theoretical centerline, or constitutes the theoretical centerline such that at least one electrode pair is disposed above the theoretical centerline and at least one electrode pair is disposed below the theoretical centerline, wherein no electrode pair, in particular, no electrode of any electrode pair is in contact with the theoretical centerline.

[0017] Advantageously, the electrodes are arranged such that they generate a substantially uniform electric field when viewed in cross-section, and in particular a partially, at least intermittently, uniform magnetic field. This electric field (potential field) advantageously extends horizontally across the entire width and depth (area) of the reactor shaft.

[0018] In one embodiment, the reactor has a reactor top and a reactor bottom, the reactor bottom also referred to as the reactor base. The reactor top and reactor bottom each have an inlet opening and an outlet opening that can be closed at least intermittently, through which at least fluid (e.g., gas or liquid) and / or solids (especially particles) can be introduced or discharged, such that, in order to generate a moving bed, particles are continuously introduced into the reactor shaft at least intermittently through the reactor top. It is also conceivable to use a fluidized bed instead of a moving bed. The moving bed advantageously conveys particles, particularly carbon-containing particles, into the reactor, particularly into the reactor shaft, and advantageously moves / conveys them through the reactor shaft – from the reactor top down to the reactor bottom. Advantageously, the particles of the moving bed or bed migrate through the reactor shaft in a gravity-driven and / or gravity-driven manner. The particles of the moving bed then receive carbon from the hydrocarbon-containing fluid introduced into the reactor shaft and advantageously transport it out of the reactor shaft through the reactor bottom. In the case of methane pyrolysis, the particles are heated, and methane preferentially decomposes on the heated particles. A portion will also decompose in the intermediate chamber and be discharged in the aforementioned manner. The continuous outward transport of carbon or carbon-containing particles ensures the maintenance of the necessary, intermittently uniform, electric field, and thus ensures a substantially uniform heat distribution, at least within the heating zone of the reactor shaft. The feed and discharge openings advantageously allow for the continuous introduction or discharge of the reactant or gas from which carbon has been removed by pyrolysis.

[0019] Another conceivable approach is to arrange the electrodes such that they generate an electric field at least partially orthogonal to the direction of movement of the moving bed through the reactor shaft. Advantageously, due to the arrangement of the electrodes in the reactor shaft, i.e., due to their arrangement at the same height on two opposing sidewalls of the reactor shaft, the electrodes generate an electric field perfectly orthogonal to the direction of movement of the moving bed (particularly the particles of the moving bed). As described above, the moving bed migrates downwards through the reactor shaft from the top, i.e., from the top of the reactor downwards to the bottom, with the particles of the moving bed introduced into the reactor shaft through the top, which can also be referred to as the reactor base. The particles of the moving bed are then discharged from the reactor shaft through corresponding outlet openings. Based on the orthogonal alignment of the electric field with respect to the particles of the moving bed, uniform heating of the particles advantageously occurs, allowing these particles to be used to receive carbon from the carbon-containing fluid across the entire plane of the reactor shaft—viewed in the cross-sectional direction. This advantageously avoids the occurrence of localized hot spots.

[0020] In a second aspect of the invention, a method is claimed for at least pyrolyzing a hydrocarbon-containing fluid (e.g., a gas or liquid) to at least produce a hydrogen-containing fluid (e.g., a gas or liquid). According to the invention, the hydrocarbon-containing fluid is countercurrently fed into a reactor shaft (also referred to as the reaction space) of the reactor along with a moving bed of particles. According to the invention, at least the particles of the moving bed or the hydrocarbon-containing fluid is heated to a defined temperature in the range of 800-1600°C, preferably 800-1500°C, more preferably 800-1400°C, by electrodes disposed in the reactor shaft for generating heat energy. More specifically, it is conceivable that the moving bed particles or hydrocarbon-containing particles, or both, i.e., the moving bed particles and the hydrocarbon-containing fluid, are heated (heated) by electrical energy generated by the electrodes. Advantageously, pyrolysis occurs, i.e., carbon and hydrogen dissociate from the hydrocarbon-containing fluid at temperatures exceeding and above about 800°C. Advantageously, the electrodes generate heat primarily through resistance (e.g., particularly the resistance of the particles in the granular bed or moving bed), as electrical energy is dissipated as heat energy.

[0021] Advantageously, the method is carried out in a reactor according to the first aspect of the invention (i.e., a reactor of the type described above). Therefore, detailed features of the first aspect of the invention, namely the reactor of the invention, are hereby fully incorporated herein.

[0022] It is conceivable that the particles in the moving bed migrate downwards from the top to the bottom of the reactor in the vertical longitudinal direction of the reactor by gravity, particularly gravity-driven. Therefore, the particles in the moving bed are fed into the reactor shaft through one or more inlet openings in the top of the reactor and migrate through the reactor shaft in the direction of the bottom of the reactor. The bottom of the reactor advantageously has one or more outlet openings through which carbon-loaded particles are advantageously discharged from the reactor shaft.

[0023] Advantageously, electrodes disposed within the reactor shaft, particularly on the side or inner wall of the reactor shaft, generate an electric field that is advantageously aligned, at least partially, orthogonal over its entire extent to the direction of movement of the particles moving through the reactor shaft. Thus, viewed in the cross-sectional direction, the electric field extends substantially horizontally. Simultaneously, viewed in the longitudinal direction or longitudinal section direction, the particles migrate substantially vertically through the reactor shaft. This advantageously enables heating of at least the particles in the moving bed, at least over its entire extent, within the heating zone of the reactor shaft, and avoids or at least counteracts the formation of localized hot spots within the reactor shaft.

[0024] In one embodiment, a first thermal integration zone, a reaction zone, a heating zone, and a second thermal integration zone are formed within the reactor shaft. Viewed vertically along the reactor's longitudinal direction, the various zones are continuous from the reactor bottom (also referred to as the reactor base) upwards to the reactor top and partially overlap. More specifically, there are overlapping areas and / or adjacent but non-overlapping areas. The heating zone is primarily formed in the area of ​​the reactor shaft where electrodes are disposed. It is conceivable that the heating zone and the reaction zone at least partially overlap. Conversely, this refers to the reaction, i.e., dissociation, particularly the separation of carbon from the hydrocarbon-containing fluid, which has occurred—at least partially—outside the heating zone, especially in the reaction zone. The various zones are further elaborated below—in the description of the accompanying drawings.

[0025] Advantageously, pyrolysis takes place at least in the reaction zone or the heating zone. More specifically, it is conceivable that pyrolysis, i.e., the decomposition of the hydrocarbon-containing fluid (especially a gas), and thus the separation of carbon from the hydrocarbon-containing fluid, occurs in the reaction zone, the heating zone, or both. Advantageously, as mentioned above, pyrolysis takes place in the overlapping region of the two zones.

[0026] Another possibility is that the hydrocarbon-containing fluid is preheated, at least in the first thermal integration zone, by particles from a moving bed that 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 blown, into the reactor shaft through the bottom of the reactor (also called the reactor base), especially via at least one feed opening. Thus, the hydrocarbon-containing fluid moves substantially vertically upward through the reactor shaft from the bottom of the reactor to the top of the reactor. This flow of the hydrocarbon-containing particles is opposite to the flow of the moving bed particles, which migrate substantially vertically downward through the reactor shaft from the top of the reactor to the bottom of the reactor. On the path of the moving bed particles through the reactor shaft, the particles have passed through at least the heating zone and absorbed heat / thermal energy in that zone before reaching the first thermal integration zone. When the moving bed particles subsequently encounter the hydrocarbon-containing fluid in the first thermal integration zone, the moving bed particles release heat (thermal energy) into the hydrocarbon-containing fluid. Thus, in the first thermal integration zone, the hydrocarbon-containing fluid is preheated before reaching the heating zone. It is conceivable that the hydrocarbon-containing fluid is preheated to a temperature between 600-800°C in the first thermal integration zone. If a temperature of at least 800°C is reached during the flow through the first thermal integration zone, a reaction zone is formed above this temperature, in which carbon separates from the hydrocarbon-containing fluid and deposits on the particles of the moving bed. Therefore, it is possible that the pyrolysis of the hydrocarbon-containing fluid has already begun in the reaction zone, which develops due to the thermal energy brought by the particles of the moving bed. Similarly, it is conceivable that the hydrocarbon-containing fluid introduced into the reactor shaft is preheated before entering and thus flows into the reactor shaft in a preheated form. Here, the hydrocarbon-containing fluid can be preheated to, for example, a temperature not exceeding 600°C, advantageously below 800°C. Therefore, the development of the reaction zone can be accelerated after the preheated hydrocarbon-containing fluid is introduced into the reactor shaft. In particular, the hydrocarbon-containing fluid preheated in the first thermal integration zone can be heated to a temperature of at least 800°C more quickly compared to the unpreheated hydrocarbon-containing fluid. Because the reaction zone develops more rapidly by reaching a pyrolysis temperature of 800°C, pyrolysis can also proceed more quickly (compared to pyrolysis with hydrocarbon-containing fluid not introduced in a preheated form), allowing the entire pyrolysis process to proceed in a more energy-efficient manner. However, if the hydrocarbon-containing fluid is preheated outside the reactor or at least outside the reactor shaft (reaction space), it must be ensured that the temperature (pyrolysis temperature) is not reached or even exceeded so that pyrolysis can take place within the reactor shaft.

[0027] Advantageously, the particles of the moving bed entering the reactor shaft are preheated at least in the second thermal integration zone by a heated hydrogen-containing fluid that flows countercurrently to the particles of the moving bed, is generated by a hydrocarbon-containing fluid, and has already passed through the heating zone and released carbon. Therefore, viewed from the top of the reactor along the direction from the bottom of the reactor, the second thermal integration zone is the zone upstream of the heating zone. Then, the hydrocarbon-containing fluid, which has separated carbon at least in the reaction zone and advantageously also in the heating zone, flows through the second thermal integration zone as a hydrogen-containing fluid, which introduces the corresponding heat (thermal energy) from the reaction zone and ultimately also introduces heat from the heating zone into the second thermal integration zone. This thermal energy is then transferred to the particles of the moving bed, which are advantageously introduced into the reactor shaft in an unpreheated form. Thus, the particles of the moving bed have been preheated by the thermal energy of the hydrogen-containing fluid in the first thermal integration zone before reaching the heating zone.

[0028] In one embodiment, the carbon-loaded particles in the moving bed are discharged from the reactor shaft via the bottom of the reactor. It is conceivable that the particles in the moving bed are sent to downstream processes for particle cleaning, i.e., removal of carbon from the particles, or to further chemical processes for further treatment. Due to the reactions that have occurred, at least some of the particles in the moving bed have increased in size. The enlarged particles, especially the larger ones, are primarily discharged from this process, while smaller particles, whose size remains unchanged, especially almost unchanged, are recycled. It is also conceivable that at least a portion of the enlarged (larger) particles are crushed and / or ground, particularly pulverized, wherein these pulverized particles are returned for further processing.

[0029] All the advantages of the reactor described for the first aspect of the invention appear in the described method.

[0030] It is obvious that, without departing from the scope of the invention, the features specified above and those to be set forth below can be used not only in the specified particular combinations, but also in other combinations or on their own. Attached Figure Description

[0031] Hereinafter, embodiments of the reactor and method of the present invention will be described in detail with reference to the accompanying drawings. The drawings are shown schematically:

[0032] Figure 1 A side view of one embodiment of the reactor of the present invention is shown in cross-section.

[0033] Figure 2 Shown in cross-section Figure 1 The diagram shows a top view of an embodiment of the reactor of the present invention.

[0034] Figure 3A front view showing the electrode arrangement of an embodiment of the reactor of the present invention is presented in cross-section.

[0035] Figure 4 A front view showing another electrode arrangement of an embodiment of the reactor of the present invention, in cross-section.

[0036] Figure 5 A front view showing another electrode arrangement of an embodiment of the reactor of the present invention, in cross-section.

[0037] Figure 6 Top views showing electrodes of different geometries, and

[0038] Figure 7 A schematic temperature profile of an embodiment of the reactor of the present invention, used to illustrate the method of the present invention, is shown. Detailed Implementation

[0039] exist Figures 1 to 7 In the figures, elements with the same function and mode of operation are assigned the same reference numerals.

[0040] Figure 1 A side view of an embodiment of the reactor 1 of the present invention is shown schematically in cross-sectional form. More specifically, this is a longitudinal section through an embodiment of the reactor 1 of the present invention. Figure 2 A cross-sectional view is shown. Figure 1 The diagram shows a top view of an embodiment of the reactor 1 of the present invention. More specifically, Figure 2 It shows Figure 1 The cross-section of an embodiment of the reactor 1 of the present invention shown herein is substantially along... Figure 1 The centerline M shown extends. Therefore, according to Figure 2 Reactor 1 is cut off in the middle (i.e., at the midpoint). Therefore, it will be described collectively below. Figure 1 and Figure 2Reactor 1 has a reactor shell 2, the cross-section of which has a circular geometry and extends like a tower in the longitudinal direction L. The reactor shell 2 is completely enclosed and therefore has a closed reactor shell wall 20, the cross-section of which is circular. A reactor shaft 3 is disposed within the reactor shell 2 or the reactor shell wall 20. The cross-section of the reactor shaft 3 has a quadrilateral geometry, particularly a square geometry, and extends like a tower in the longitudinal direction L. Therefore, the reactor shaft 3 includes at least four sidewalls 30, 31, 32, 33, particularly the shaft walls 30, 31, 32, 33. At least two of the sidewalls 30, 31, 32, 33, particularly the first sidewall 30 and the third sidewall 32, are parallel to each other. The reactor shaft 3 is a reaction space, which therefore has a reaction chamber 34, within which chemical reactions, particularly the pyrolysis of hydrocarbon-containing fluids (mainly hydrocarbon-containing gases), occur. A reactor liner 4 is provided between the reactor shaft 3, and particularly the sidewalls 30, 31, 32, and 33 of the reactor shaft 3, and the reactor shell 2, particularly the reactor shell wall 20. This reactor liner 4 advantageously extends completely along the circumferential and longitudinal directions L between the reactor shaft 3 and the reactor shell 2. The reactor liner 4 primarily serves to protect the reactor shell from the heat energy introduced into the reaction chamber 34 of the reactor shaft 2. Furthermore, Figure 1 and Figure 2 A total of six electrodes 10, 11, 12, 13, 14, and 15 are shown, disposed on the reactor shaft 3, and more specifically on the first sidewall 30 and the third sidewall 32 of the reactor shaft 3. Accordingly, three electrodes 10, 12, and 14 are disposed on the first sidewall 30, while the other three electrodes 11, 13, and 15 are disposed on the third sidewall 32. Advantageously, each electrode 10, 11, 12, 13, 14, and 15 extends over the entire width of the sidewalls 30 and 32 when viewed in the cross-sectional direction. The second sidewall 31 and the fourth sidewall 33 are substantially free of electrodes. Opposite 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 form the second electrode pair 102, and electrodes 14 and 15 form the third electrode pair 103. Advantageously, when viewed in the longitudinal direction L, the electrodes 10, 11, 12, 13, 14, and 15 of electrode pairs 101, 102, and 103 are at the same height. The reference numeral M indicates the characteristic of the centerline. Therefore, this (theoretical) centerline M defines the middle of reactor 1, and especially reactor shaft 3, when viewed along the longitudinal direction L. Electrodes 10, 11, 12, 13, 14, and 15 are mainly located in the region of centerline M, particularly near centerline M. Specifically, as... Figure 1As shown, the first electrode pair 101, consisting of at least electrodes 10 and 11, is in partial contact with the centerline. Conversely, the second electrode pair 102, consisting of electrodes 12 and 13, and the third electrode pair 103, consisting of electrodes 14 and 15, are offset above the centerline M, i.e., offset towards the reactor top 5 of the reactor 1, particularly in the portion of the reactor shaft 3 extending between the centerline M and the reactor top 5. Conversely, the portion of the reactor shaft 3 extending from the centerline M towards the reactor bottom 6 does not have additional electrode pairs. The arrangement of electrodes 10, 11, 12, 13, 14, and 15 within the reactor shaft 3 relative to the height of the reactor shaft 3 extending longitudinally L can be individually designed and determined by the desired location of the heating zone and the resulting reaction zone. More specifically, the positioning of electrodes 10, 11, 12, 13, 14, and 15 also depends accordingly on whether the heating zone is formed in the upper or lower region of the reactor shaft 3 relative to the centerline M. The variable positioning of electrodes 10, 11, 12, 13, 14, and 15 is also shown below. Figure 3 , Figure 4 and Figure 5 As shown in the image.

[0041] Figure 3 , Figure 4 and Figure 5 Each cross-sectional view shows a front view of the electrode arrangement in one embodiment of the reactor 1 of the present invention.

[0042] like Figure 3 As shown, the three electrode pairs 101, 102, and 103 used here are positioned within the reactor shaft 3 such that the electrode of the second electrode pair 102 is at least partially in contact with the (theoretical) centerline M, and is therefore positioned in the middle of the reactor shaft 3 in at least a portion of its length. The remaining electrode pairs 101 and 103 are then positioned within the reactor shaft 3 at a certain distance from the centerline M. Thus, the electrode 101 of the first electrode pair is positioned in the region of the reactor shaft 3 between the centerline M and the reactor bottom 6, i.e., in the lower region relative to the centerline M, while the electrode of the third electrode pair 103 is positioned in the region of the reactor shaft 3 between the centerline M and the reactor top 5, i.e., in the upper region relative to the centerline M.

[0043] like Figure 4As shown, it is also conceivable to have only two electrode pairs 101 and 102 arranged, wherein neither of the electrode pairs 101 nor 102, and especially neither of the electrodes of the respective electrode pairs 101 and 102, is in even partial contact with 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., the upper region relative to the centerline M, while 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 top 5, i.e., the upper region relative to the centerline M.

[0044] like Figure 5 As shown, it is also conceivable to construct a single electrode pair 101. In this case, the respective electrode of the electrode pair 101 is at least partially in contact with the (theoretical) centerline M, and advantageously extends across the centerline M into the upper region of the reactor shaft 3 formed between the centerline M and the reactor top 5, and also into the lower region of the reactor shaft 3 formed between the centerline M and the reactor bottom 6. The electrodes of the electrode pair 101 are mainly arranged such that a large area of ​​the respective electrode of the electrode pair 101 exists in the upper region of the reactor shaft 3. Therefore, the electrodes of the electrode pair 101 (i.e., electrode sub-101) are positioned slightly upwardly offset relative to the centerline M.

[0045] It is conceivable that the positions and numbers of electrode pairs 101, 102, and 103 can be substituted. This means that more than three electrode pairs 101, 102, and 103 can also be set within reactor shaft 3. However, not only the number and location of electrode pairs 101, 102, and 103 within reactor shaft 3 can be varied.

[0046] like Figure 6 As shown, electrodes 10, 11, 12, 13, 14, and 15 can also have different geometries. For example, it is conceivable to use mesh electrodes 16 or circular electrodes 17, as well as quadrilateral, especially rectangular, electrodes 18 and 19. The dimensions of electrodes 16, 17, 18, and 19 can also be different. For example, the dimensions of a rectangular, large-area electrode 19 can be such that it substantially comprises the dimensions of at least two, especially three or more, rectangular electrodes 18, and thus can be arranged individually or together with electrodes 19 of the same geometry in the reactor shaft to create electrode pairs. Using or arranging multiple electrode pairs 101, 102, and 103 within the reactor shaft 3 advantageously allows for the establishment of different axial temperature zones. Therefore, it is advantageous to controllably regulate the temperature via field parameters, given the different resistance characteristics of the particulate material in the moving bed.

[0047] Figure 7A schematic temperature profile of an embodiment of the reactor 1 of the present invention, used to illustrate the method of the present invention, is shown. (In conjunction with, for example...) Figure 1 and Figure 2 The basic structure of reactor 1 shown is used to illustrate this. Figure 7 Temperature curves are plotted. Temperatures are shown on the x-axis of the temperature curves. Thresholds of 800°C and 1500°C are specified by way of example. The axial range of reactor shaft 3 in the longitudinal direction L is shown on the y-axis. Figure 7The exothermic reaction occurs in the reaction chamber 34 of the vertical shaft 3 of the reactor 1 of the present invention. Hydrocarbon-containing fluid 40 is introduced into the reactor shaft 3, particularly into the reaction chamber 34 of the reactor shaft 3, via an inlet / feed opening (not shown) in the bottom 6 of the reactor, and particles 50 of the moving bed are introduced through an inlet / feed opening (not shown) in the top 5 of the reactor. The hydrocarbon-containing fluid 40 flows through the reactor shaft 3 from the bottom 6 towards the top 5. The particles 50 of the moving bed migrate through the reactor shaft 3 in the opposite direction from the top 5 towards the bottom 6. The hydrocarbon-containing fluid 40 may be preheated before entering the reactor shaft 3. The possible temperature is below 800°C, particularly approximately 600°C. However, it is also conceivable that the hydrocarbon-containing fluid 40 may be introduced into the reactor shaft 3 without preheating. Simultaneously, the moving bed particles 50 are also introduced into the reactor shaft 3, and migrate through the second thermal integration zone W2, the heating zone B, the reaction zone R, and the first thermal integration zone W1 as they descend through the reactor shaft 3 to the reactor bottom 6. In the second thermal integration zone W2, formed between the heating zone B and the reactor top 5, the moving bed particles 50 are preheated within the reactor shaft 3. This is achieved by transferring thermal energy from heated hydrogen-containing gas 41 to the moving bed particles 50, which exits the reactor shaft 3 from the heating zone B via an outlet / discharge opening (not shown) in the reactor top 5. Thus, in the second thermal integration zone W2, thermal / thermal energy integration from the gas phase to the solid phase advantageously occurs. The hydrogen-containing gas 41 is a reaction product formed by the pyrolysis of the hydrocarbon-containing fluid 40 introduced into the reactor shaft 3. Pyrolysis advantageously occurs in the reaction zone R, and at least partially in the heating zone B, and advantageously (also) in the overlapping region of the reaction zone R and the heating zone B. To initiate pyrolysis, i.e., the thermal dissociation of hydrocarbons into carbon and hydrogen components, and thus the separation of carbon from the hydrocarbon-containing fluid 40, a minimum temperature of approximately 800°C is required. Advantageously, this minimum temperature is already reached after passing through the first thermal integration zone W1. In this first thermal integration zone W1, thermal energy begins to transfer from the loaded particles 51 of the moving bed, which have migrated through the heating zone B on their way to the reactor bottom 6. Thus, in the first thermal integration stage W1, the integration of heat / thermal energy from the solid phase to the gas phase advantageously occurs. The closer the hydrocarbon-containing fluid 40 gets to the heating zone B, the hotter it becomes, because it constantly absorbs thermal energy through the loaded particles 51 of the moving bed. In the context of this invention, the loaded particles 51 of the moving bed should be understood as particles that have received carbon or carbon atoms from the hydrocarbon-containing fluid 40. Carbon is mainly deposited on and between the particles 50 of the moving bed. This deposition affects the characteristics of the moving bed, or the bed resistance characteristics of the moving bed that migrates by gravity through the reactor shaft 3. Figure 1The exemplary arrangement of electrodes 10, 11, 12, 13, 14, 15 within the at least square reactor shaft 3, the resulting potential field, and the flow direction of the moving bed, or particles 50 within the moving bed, moves new particulate material into the heating zone B, thus preventing any adverse effects on the resistivity characteristics. In the context of this invention, the heating zone B should be understood as the area where electrodes 10, 11, 12, 13, 14, 15 are at least partially, advantageously, completely positioned or disposed. More specifically, electrodes 10, 11, 12, 13, 14, 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 heating to approximately 800°C of the hydrocarbon-containing fluid, the pyrolysis process thus begins and a reaction zone R is formed. This refers to the migration of carbon from the hydrocarbon-containing fluid 40 in the direction of the particles 50 in the moving bed, or at least partially loaded particles 51. The chemical reaction process can also begin upstream of the heating zone B, thus heating the hydrocarbon-containing fluid 40 solely by the thermal energy of the loaded particles 51 of the moving bed before reaching the region formed by electrodes 10, 11, 12, 13, 14, and 15. Within the heating zone B, the particles 50 of the moving bed, and therefore the hydrocarbon-containing fluid 40, are heated to a maximum temperature advantageously between 1200°C and 1700°C. Pyrolysis occurs within this heating zone B until substantially all the carbon has been transferred from the hydrocarbon-containing fluid 40 to the particles 50 of the moving bed. The remainder is the hydrogen-containing fluid 41 and the loaded particles 51 of the moving bed, or at least partially loaded particles 51. Therefore, it is conceivable that the chemical reaction is completed even before the hydrocarbon-containing fluid 40 has completely flowed through the heating zone B. Thus, it is conceivable that the reaction zone R does not additionally encompass the entire length of the heating zone B, but only partially overlaps with it.

[0048] Appendix Label Table

[0049] 1. Reactor

[0050] 2 Reactor shell

[0051] 3. Reactor shaft

[0052] 4. Reactor Lining

[0053] 5. Top of reactor

[0054] 6. Bottom of the reactor

[0055] Electrodes 10, 11, 12, 13, 14, and 15

[0056] 16 Mesh Electrodes

[0057] 17 Circular Electrode

[0058] 18 Quadrilateral / Rectangular Electrodes

[0059] 19 Quadrilateral Large Electrode

[0060] 20 Reactor shell wall

[0061] 30, 31, 32, 33 Reactor shaft wall / sidewall

[0062] 34 Reaction Chamber

[0063] 40 Hydrocarbon-containing fluids

[0064] 41 Hydrogen-containing fluids

[0065] 50 Unloaded particles in a moving bed

[0066] 51 Loaded particles in a moving bed

[0067] Electrode pairs 101, 102, and 103

[0068] B Heating Zone

[0069] L (vertical direction)

[0070] M centerline

[0071] R Reaction Zone

[0072] W1 First Hot Integration Zone

[0073] W2 Second Hot Integration Zone

[0074] x and y axes.

Claims

1. A reactor (1) for pyrolyzing a hydrocarbon-containing fluid (40) to produce a hydrogen-containing fluid (41), wherein, The reactor (1) has a reactor shell (2) and a reactor shaft (3) disposed within the reactor shell (2), and a reactor liner (4) is disposed between the reactor shell (2) and the reactor shaft (3) for heat-sealing the reactor shaft (3) relative to the reactor shell (2). Its features are, The reactor shell (2) of the reactor has an annular or circular cross-sectional geometry, and the reactor shaft (3) has a quadrilateral or multi-sided polygonal geometry in cross-section, wherein at least one electrode (10, 11, 12, 13, 14, 15) for generating heat energy is disposed on each of two opposing sidewalls (30, 31, 32, 33) of the reactor shaft (3).

2. The reactor (1) according to claim 1, Its features are, When viewed in the vertical longitudinal direction (L) of the reactor (1), the electrodes (10, 11, 12, 13, 14, 15) that are opposite to each other are at least partially located in the middle of the reactor shaft (3).

3. The reactor (1) according to any one of claims 1-2. Its features are, Two or more electrodes (10, 11, 12, 13, 14, 15) for generating heat energy are provided on each of the two opposing sidewalls (30, 31, 32, 33) of the reactor shaft (3), wherein, viewed in the vertical longitudinal direction (L) of the reactor (1), at least one of the electrodes (10, 11, 12, 13, 14, 15) of each sidewall (30, 31, 32, 33) of the reactor shaft (3) is at least partially located in the middle of the reactor shaft (3), or each of the electrodes (10, 11, 12, 13, 14, 15) of each sidewall (30, 31, 32, 33) is at least located above or below the middle of the reactor shaft (3).

4. The reactor (1) according to any one of claims 1-2. Its features are, The electrodes (10, 11, 12, 13, 14, 15) are arranged such that the electrodes generate a partially uniform electric field that is observed at least intermittently in cross-section.

5. The reactor (1) according to any one of claims 1-2. Its features are, The reactor (1) has a reactor top (5) and a reactor bottom (6), wherein the reactor top (5) and the reactor bottom (6) each have an inlet opening and an outlet opening that can be closed at least intermittently, through which solids in the form of at least fluid or particles can be introduced or discharged, such that in order to generate a moving bed, particles (50) are continuously introduced into the reactor shaft (3) at least intermittently through the reactor top (5).

6. The reactor (1) according to claim 5, Its features are, The electrodes (10, 11, 12, 13, 14, 15) are arranged such that they generate an electric field that is at least partially orthogonal to the direction of movement of the moving bed through the reactor shaft (3) of the particles (50).

7. A method for pyrolyzing a hydrocarbon-containing fluid (40) to produce a hydrogen-containing fluid (41), wherein, The hydrocarbon-containing fluid (40) is fed countercurrently into the reactor shaft (3) of the reactor (1) along with the moving bed of the reactor composed of particles (50). Its features are, At least the particles (50) of the moving bed or the hydrocarbon-containing fluid (40) are heated to a defined temperature in the range of 800-1600°C by electrodes (10, 11, 12, 13, 14, 15) provided in the reactor shaft for generating heat energy, the method being carried out in the reactor (1) according to any one of claims 1 to 6.

8. The method according to claim 7, Its features are, At least the particles (50) of the moving bed or the hydrocarbon-containing fluid (40) are heated to a defined temperature in the range of 800-1400°C by electrodes (10, 11, 12, 13, 14, 15) provided in the reactor shaft for generating heat energy.

9. The method according to claim 7, Its features are, The particles (50) of the moving bed migrate by gravity from the top (5) of the reactor (1) to the bottom (6) of the reactor (1) in the vertical longitudinal direction (L).

10. The method according to any one of claims 7-9, Its features are, The electrodes (10, 11, 12, 13, 14, 15) generate an electric field that is at least partially orthogonal to the direction of movement of the particles (50) through the reactor shaft (3) of the moving bed.

11. The method according to any one of claims 7-9, Its features are, A first thermal integration zone (W1), a reaction zone (R), a heating zone (B), and a second thermal integration zone (W2) are formed within the reactor shaft (3). When viewed in the vertical longitudinal direction (L) of the reactor (1), from the bottom (6) of the reactor (1) to the top (5) of the reactor (1), the zones are continuous and at least partially overlap.

12. The method according to claim 11, Its features are, The pyrolysis shall be carried out at least in the reaction zone (R) or the heating zone (B).

13. The method according to claim 11, Its features are, The hydrocarbon fluid (40) has been preheated at least in the first thermal integration zone (W1) by the particles (51) of the moving bed that have passed through the heating zone (B) and moved countercurrently with the hydrocarbon fluid (40).

14. The method according to any one of claims 12 to 13, Its features are, The particles (50) entering the reactor shaft (3) of the moving bed have been preheated by heated hydrogen-containing fluid (41) in at least the second thermal integration zone (W2), the heated hydrogen-containing fluid (41) flowing countercurrently to the particles (50) of the moving bed, generated by the hydrocarbon-containing fluid (40) and having passed through the heating zone (B) and released carbon.

15. The method according to any one of claims 12-13, Its features are, The carbon-loaded particles (51) in the moving bed are discharged from the reactor shaft (3) via the reactor bottom (6) of the reactor (1).

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