Reactors for endothermic high-temperature reactions

Abstract

The present invention relates to a reactor (1) for carrying out endothermic reactions, particularly high-temperature reactions, in which a product gas (P) is obtained from a feed gas (E), the reactor (1) encloses a reactor interior (10), the reactor (1) is configured to provide a reactor bed (120) in a reaction zone (12) of the reactor interior (10), the reactor bed containing a number of solid material particles (F), the reactor (1) is also configured to introduce the feed gas (E) into the reaction zone (12), and in order to heat the feed gas (E), the reactor (1) is designed to heat the solid material particles (F) in the reaction zone (12), thereby transferring heat from the solid material particles (F) to the feed gas (E) and thereby raising the feed gas (E) in the reaction zone (12) to a reaction temperature or higher. The reactor interior (10) also comprises a first heat-integration zone (11) in which heat from the product gas (P) produced in the reaction zone (12) can be transferred to the solid material particles (F) in the reactor bed (120) and the solid material particles are introduced into the reaction zone (12). The reactor interior (10) also comprises a second heat-integration zone (13) in which heat from the solid material particles (F) in the reactor bed (12) coming from the reaction zone (12) can be transferred to the feed gas (E) and the feed gas (E) can be preheated. The present invention also relates to a method of using the reactor (1) according to the present invention.

Description

[Technical Field]

[0001] The present invention relates to a reactor for endothermic high temperature reactions, such as a reactor for steam reforming of a hydrocarbon-containing feed gas stream (e.g., containing methane), or for example, a reactor for cracking or thermal cracking of ethane, or for example, a reactor for thermal cracking of natural gas (e.g., containing methane).

[0002] Fossil fuels are burned in furnaces or reactors for ethane cracking or methane steam reforming to generate thermal energy, e.g., to heat the respective feed stream or process gas by indirect heat transfer. Combustion of fossil fuels inevitably produces CO2 emissions. Energy efficiency is generally increased by preheating the combustion air, preheating the feed, and / or transferring heat from the hot process gas to a boiler feedwater to generate process steam.

[0003] As an alternative to established prior art, U.S. Patent No. 2,982,622, for example, discloses a method for producing hydrogen and high-quality coke. In the method, particles of inert solid material are passed as bulk material through an elongated reaction zone in the direction of gravity, and an electrical voltage of 0.1 to 1000 volts per inch is applied across at least a portion of the mass of solid material in the reaction zone, sufficient to raise the temperature of the solids to 1800°F to 3000°F (980°C to 1650°C). A gas stream of hydrocarbons, preferably natural gas, is introduced countercurrently, and this gas stream produces hydrogen by endothermic pyrolysis reactions and deposits carbon on the introduced particles. CH4<->C(s)+2H2.

[0004] Countercurrent solid and gas flows allow for heat integration and promote high process efficiency. When using renewable current, ohmic direct electrical heating can improve the CO2 balance of hydrogen production processes by eliminating fossil heating. Summary of the Invention [Problem to be solved by the invention]

[0005] In this regard, however, research has shown that carbon that separates from the gas phase reduces the pourability of the inert solid material particles and causes blocking of the bulk material after prolonged operation, significantly limiting the economic efficiency of such processes.

[0006] Starting there, it is an object of the present invention to provide an improved reactor which eliminates fossil heating of the endothermic reaction and at the same time allows for efficient operation of the reactor.

[0007] This object is achieved by a reactor having the features of claim 1. Advantageous embodiments of the invention are defined in the associated dependent claims and are explained below.

[0008] In reactors for carrying out endothermic reactions, in particular high temperature reactions, the product gas is obtained from the feed gas in the reactor, which preferably encloses a reactor interior which is divided into three zones: a first heat-integration zone, a reaction zone, and a second heat-integration zone. The reactor is configured to guide a moving bed in the direction of gravity, the moving bed consisting of a plurality of solid material particles, which are added to an upper end of the reactor and removed at a lower end of the reactor. The reactor is further configured to guide a feed gas through a reaction zone. The reactor for heating the feed gas is configured to heat the solid material particles in the reaction zone (e.g., by generating an electric current in the solid material particles, i.e., by generating Joule heat in the solid material particles), thereby transferring heat from the solid material particles to the feed gas, thereby heating the feed gas in the reaction zone to a reaction temperature that can participate as a starting product in an endothermic reaction to produce a product gas. The reactor interior also includes a first heat-integration zone, in which heat from the product gas produced in the reaction zone can be transferred to the solid material particles in the reactor bed, leading to the solid material particles being guided to the reaction zone. The interior also includes a second heat-integration zone, in which heat from the solid material particles in the reactor bed coming from the reaction zone can be transferred to the feed gas, allowing the feed gas to be preheated.

[0009] According to one embodiment of the reactor, it is provided that the reactor for heating solid material particles in a moving bed comprises a first electrode and a second electrode, in particular the first electrode is arranged above the second electrode inside, in particular the two electrodes are permeable to the solid material particles, the feed gas and the product gas, respectively, i.e. the two electrodes are arranged or configured such that the solid material particles, the feed gas and the product gas can pass through the electrodes inside the reactor without impairing the fluidity of the solid material particles.

[0010] According to one embodiment of the reactor, the first and / or second electrodes may include one or more posts extending through the reactor interior.

[0011] Furthermore, according to one embodiment, it is provided that the first electrode comprises or is formed by a grid, and the second electrode may also comprise or be formed by a grid.

[0012] Furthermore, according to an embodiment of the present invention, it is provided that the first electrode and / or the second electrode (or the posts or grids of the first electrode and / or the second electrode, respectively) comprises or consists of one of the following materials: high temperature resistant steel, Ni-containing steel alloy (e.g. Centralloy G 4852 Micro R), nickel-based alloy, silicon carbide, molybdenum disilicide, graphite.

[0013] In principle, materials characterized by high temperature resistance (chemical and mechanical stability at high temperatures) and the highest possible electrical conductivity are preferred. In the case of graphite, its chemical stability in the presence of water vapor and at high temperatures can be improved, for example, by a protective coating.

[0014] Also, in one embodiment, it is provided that the electrodes, the electrical supply to the electrodes, and the moving bed are electrically insulated from the pressure jacket of the reactor, for example, by a slightly electrically conductive high-temperature lining, for example made of Al2O3 or ZrO2.

[0015] Furthermore, an embodiment of the present invention provides that the reactor is configured to supply or apply a DC voltage between the two electrodes to heat the solid material particles.

[0016] In one embodiment of the reactor, the reactor further comprises a solid material particle inlet through which solid material particles can be introduced into the first heat-integration zone, thereby allowing the solid material particles to be introduced through the first electrode into the reaction zone and through the second electrode into the second heat-integration zone.

[0017] One embodiment of the reactor further provides that the reactor has a solid material particle outlet (e.g., a cellular wheel sluice) through which solid material particles can be removed from the second heat-integration zone, which is the critical control factor for the moving bed velocity or mass flow rate.

[0018] One embodiment of the reactor further provides that the reactor comprises a feed gas inlet through which a feed gas can be introduced into the second heat-integration zone and from the second heat-integration zone through the second electrode into the reaction zone.

[0019] One embodiment of the reactor further provides that the reactor has a product gas outlet through which product gas produced in the reaction zone can be removed from the first heat-integration zone.

[0020] In one embodiment of the reactor, it is further provided that the reactor is configured to direct the solid material particles of the first and / or second heat-integration zones driven by gravity in the form of a moving bed.

[0021] According to a further embodiment of the reactor, it is provided that the reactor is configured to direct the solid material particles in the reaction zone driven by gravity in the form of a moving bed.

[0022] One embodiment of the reactor further provides that the reaction zone of the reactor is bounded by a peripheral wall of the reactor, which includes an inner surface facing the reaction zone, the inner surface having a conical design, so that the reaction zone tapers vertically upward. According to one embodiment, the inner surface may form an angle with a horizontal cross section of the reaction zone, the angle preferably ranging from 85° to 89.5°, preferably from 87° to 89°.

[0023] A further aspect of the invention relates to a method for carrying out an endothermic reaction to obtain a product gas from a feed gas using a reactor according to the invention. directing the plurality of solid material particles to a first heat-integration zone and from the first heat-integration zone to a reaction zone; heating the solid material particles in a reaction zone; conducting the solid material particles from the reaction zone to a second heat-integration zone and removing them from the second heat-integration zone; introducing a feed gas into a second heat-integration zone and from the second heat-integration zone into a reaction zone, heating the feed gas of the second heat-integration zone relative to the solid material particles coming from the reaction zone to cool the solid material particles, contacting the feed gas of the reaction zone with the heated solid material particles and transferring heat from the heated solid material particles to the feed gas so as to heat the feed gas of the reaction zone, and participating the feed gas of the reaction zone as a starting product in the reaction by producing a product gas; directing the generated product gas from the reaction zone to a first heat-integration zone, preheating the solid material particles in the first heat-integration zone relative to the product gas coming from the reaction zone, and cooling the product gas; A product gas is removed from the first heat integration zone.

[0024] In a method according to one embodiment, the solid material particles are preferably recycled, i.e. in particular the solid material particles removed from the second heat-integration zone are returned to the first heat-integration zone (possibly after intermediate treatment of the solid material particles).

[0025] According to a further embodiment of the method, the feed gas is ethane (C2H6) together with water vapor (H2O), which is converted in a reaction zone, preferably at a temperature of about 850°C to 1250°C and a pressure of 1 to 5 bar(a), to ethene (C2H4) and hydrogen (H2) as product gases, and ceramic spheres, for example made of corundum (Al2O3), are used as the solid material particles.

[0026] According to a further embodiment of the method, the endothermic reaction is steam reforming. CH4 + H2O → CO + 3H2, wherein methane (CH4) as a feed gas is reacted with water vapor (HO) in a reaction zone (preferably at a temperature of about 950°C to 1250°C and a pressure of 10 bar(a) to 100 bar(a), preferably at a pressure of 15 bar(a) to 50 bar(a)) to form carbon monoxide and hydrogen as product gases, and ceramic spheres made of, for example, corundum (Al2O3) are preferably used as the solid material particles, or again, an attrition-resistant Ni-based catalyst.

[0027] Additionally, the reaction according to one embodiment may also be a reverse water gas shift reaction. CO2+H2→CO+H2O, where CO2 and H2 are reacted as feeds to form CO and H2O, and ceramic spheres made from, for example, corundum (Al2O3) are again used as the solid material particles, or attrition-resistant Ni-based catalyst.

[0028] In principle, the reaction can also be a steam cracking reaction using naphtha as feed.

[0029] Furthermore, the reaction according to one embodiment may be propane dehydration to form propene (C3H8 → C3H6 + H2), where propane is used as the feed and the solid material particles in the reactor bed form a suitable catalyst for the reaction. The catalyst requires increased attrition resistance compared to tubular fixed-bed reactors, but advantageously allows for external catalyst regeneration in the event of coking due to the reaction.

[0030] Additionally, according to one embodiment, the reaction also includes butane dehydration (CH) to form butenes. 10 →C4H8+H2), butane is used as the feed, and the solid material particles in the reactor bed again form a suitable catalyst for the reaction.

[0031] Furthermore, the reaction according to one embodiment may also be butene dehydration (C4H8 → C4H6 + H2) to form butadiene, with butene being used as the feed and the solid material particles in the reactor bed again forming a suitable catalyst for the reaction.

[0032] Additionally, the reaction according to one embodiment involves the dehydration of ethylbenzene (CH) to form styrene. 10 →C8H8+H2), ethylbenzene is used as the feed, and the solid material particles in the reactor bed again form a suitable catalyst for the reaction. [Brief explanation of the drawings]

[0033] Further features and advantages of the invention are explained in the description of exemplary embodiments with reference to the figures, in which:

[0034] [Figure 1] FIG. 1 is a schematic diagram of one embodiment of the reactor according to the invention or the method according to the invention.

[0035] [Figure 2] FIG. 2 is a schematic diagram of a further embodiment of the method according to the invention.

[0036] [Figure 3] FIG. 3 is a schematic diagram of one embodiment of the reaction zone of a reactor according to the invention or of the process according to the invention. DETAILED DESCRIPTION OF THE INVENTION

[0037] The present invention, in different embodiments or applications, relates to a reactor 1 for carrying out an endothermic reaction, as shown in Figures 1 to 3.

[0038] The reactor 1 is configured to perform an endothermic reaction from a feed gas E to obtain a product gas P. In this respect, Figure 1 shows a variant in which ethane as feed gas E is reacted to form ethene (C2H4) and hydrogen (H2) as product gas P. Alternatively, according to Figure 2, the reactor can also be used, for example, for steam reforming, in which methane (CH4) as feed gas is reacted with steam (H2O) to form carbon monoxide and hydrogen as product gas P or synthesis gas. Other reactions are also possible.

[0039] 1 to 3, the reactor 1 each surrounds a reactor interior 10, and the reactor 1 is configured to provide a reactor bed 120 containing a plurality of solid material particles F in a reaction zone 12 of the reactor interior 10. The reactor 1 is further configured to introduce a feed gas E into the reaction zone 12, and the reactor 1 for heating the feed gas E is configured to heat the solid material particles F in the reaction zone 12, so that the feed gas E in the reaction zone 12 is heated to a reaction temperature by transferring heat from the solid material particles F to the feed gas E, thereby producing a product gas P. The reactor interior 10 also includes a first heat-integration zone 11 in which heat from the product gas P produced in the reaction zone 12 can be transferred to the solid material particles F in the reactor bed 120 to direct the solid material particles to the reaction zone 12, and a second heat-integration zone 13 in which heat from the solid material particles F in the reactor bed 120 coming from the reaction zone 12 can be transferred to the feed gas E to preheat the feed gas E.

[0040] In the embodiment of the reactor 1 shown in FIGS. 1 and 2, the reactor bed 120 of the reaction zone 12 and the reactor beds 110, 130 of the heat integration zone are gravity-driven solid material particles F, and the feed gas E forms a countercurrent gas flow, so that preferably nearly perfect heat integration can be achieved.

[0041] According to one embodiment, the heating and cooling of the gas is carried out on a time scale of 0.1 seconds to 1 second, which is advantageous for reaction control, for example, when rapid cooling of the product gas to a lower temperature is required.

[0042] 1 and 2, direct electrical (or inductive) heating of the solid material particles F is used to heat the feed gas E. For this purpose, corresponding permeable electrodes 20, 21, in particular in the form of grids 20, 21, can be used, to which an electrical voltage 22 is applied, so that the resistance of the solid material particles F (mainly the solid-solid contact resistance instead of the material resistance) is used for heat generation / dissipation.

[0043] In order to achieve optimal heat integration, according to a preferred embodiment, the heat capacity flows of the gas and solid material particles E, P, F are matched to one another, resulting in so-called heat integration zones 11, 13 in the reactor interior 10 or in the moving beds 110, 130, in which the feed gas E is preheated by the hot solid material particles F from the reaction zone 12 (second lower heat integration zone 13), and the hot product gas P heats the cold solid material particles F introduced into the upper side of the reactor 1.

[0044] 1 and 2, it is preferably provided here that, when the reactor 1 is arranged as intended, the reaction zone 12 is arranged vertically between two electrodes 20, 21, the first heat integration zone 11 being arranged above the first electrode 20 and the second heat integration zone 21 being arranged below the second electrode.

[0045] It is further provided that, for the introduction of solid material particles F forming the respective reactor beds 110, 120, 130, each reactor 1 is provided with a solid material particle inlet 30, through which the solid material particles F can be introduced into the first heat-integration zone 11, so that the solid material particles F can be led through the first electrode 20 to the reaction zone 12 and through the second electrode 21 to the second heat-integration zone 13.

[0046] For removing the solid material particles F (in particular for recycling the solid material particles F to the solid material particle inlet 30), the reactor 1 also comprises a solid material particle outlet 31, via which the solid material particles F can be removed from the second heat-integration zone 13.

[0047] Furthermore, in particular, each reactor 1 for introducing a feed gas E into the reactor interior 10 comprises a feed gas inlet 32, through which the feed gas E can be introduced into the second heat integration zone 13 and from there through the second electrode 21 into the reaction zone 12.

[0048] To remove the product gas P, each reactor 1 is finally provided with a product gas outlet 33 via which the product gas P produced in the reaction zone 12 can be removed from the first heat-integration zone 11.

[0049] According to one embodiment of the present invention, at least 90% of the heat used can be recovered during the production of ethylene according to Figure 1, where for the purposes of the calculation, solid material particles F consisting of carbon are assumed. However, it is preferred to use a ceramic material instead of carbon. In particular, the present invention allows for the use of solid material particles F consisting of, for example, Al2O3 as a constituent of the reactor bed.

[0050] To achieve the aforementioned heat recovery, feed gas (ethane) E, e.g., at a temperature of 150°C and a pressure of 2 bar, can be introduced into reactor 1 at a mass flow rate of 1000 kg / h. Feed gas E can be diluted with steam at a temperature of 155°C, a pressure of 2 bar, and a mass flow rate of 300 kg / h. The reaction of ethane to form ethylene can be carried out in the reaction zone at a temperature of 850°C, e.g., and ethylene product can be removed from reactor 1 at a temperature of 150°C, a pressure of 2 bar, and a mass flow rate of 606 kg / h. Solid material particles F can also be fed to reactor 1 at a temperature of 174°C, a pressure of 2 bar, and a mass flow rate of 2.9 t / h, and removed from reactor 1 at a temperature of 280°C.

[0051] Given a conversion of ethane feed to form ethylene of 65% (feed is steam diluted with 30% steam), the heating power is 1550 kWh / t ethylene product. Assuming an electrical energy conversion efficiency of 90%, the electrical consumption is 1722 kWh / t ethylene product.

[0052] In a manner similar to that for ethane cracking, the reactor 1 according to the invention according to FIG. 2 or the method according to the invention can also be used for steam methane reforming. Instead of inert particles, a catalyst can also be used as the solid medium or solid material particles F of the moving beds 110, 120, 130. The catalyst must be more resistant to attrition than in a tubular fixed-bed reactor, but external catalyst regeneration is advantageously possible. The decision as to whether to use inert particles or reaction-influencing particles can be based, inter alia, on the reaction temperature. Taking steam reforming as an example, for example, catalytic materials can be used in the low-temperature range (approximately 950°C), while in the high-temperature range (approximately 1250°C), the reaction occurs sufficiently quickly that inert materials can be used.

[0053] According to one embodiment, the reactor is configured to guide the solid material particles F through the reaction zone 12 or the heat-integration zones 11, 13 at a defined velocity, this velocity of the solid material particles F (for example in the embodiment according to Figures 1 and 2) preferably being in the range of 0.1 m / h to 2 m / h, which represents a slow and very material-friendly velocity with a correspondingly low risk of friction-related damage to the reactor.

[0054] Direct electrical heating of the moving carbon bed 120 from about 800°C to -1250°C by the electrodes 20, 21 is possible with an electrical resistance in the range of about 1.0 ohm to 10 ohms. For this purpose, a resistance of about 0.005 to 0.04 ohms is used. * Solid material particles F in the form of carbon particles having a specific resistance of 0.15 to 1.000 m can be used, for example, at temperatures in the range above 800°C.

[0055] The solid material particles F of the moving beds 110, 120, and 130 must be sufficiently chemically stable under the reaction conditions. Therefore, ceramic materials are preferred over carbon when water vapor or higher amounts of CO2 are present in the exhaust gas. The respective solid material media F can be selected depending on the process requirements. In principle, low-impedance materials, such as ceramic materials, are advantageous. Their electrical conductivity should preferably be higher than that of the refractory lining material of the reactor 1, so that heating of the reactor bed 120, rather than the surrounding refractory material, is primarily performed. When materials with relatively high conductivity are used, the boundary resistance between individual solid material particles F is particularly important for the overall resistance. Therefore, the surface morphology can be adjusted to require increased electrical resistance. According to one embodiment, the solid material particles are, for example, non-spherical particles.

[0056] The length of the reaction zone 12 in the vertical or flow direction of the solid material particles F and feed gas stream E defines the residence time of the gas in the heating zone 12. The longer the length, the more favorable the conditions for electrical heating, since the overall electrical resistance (series contact resistance of the particles F) will be correspondingly higher. Residence times of less than 1 second in the reaction zone 12 are possible, which is favorable for ethylene production by ethane dehydration.

[0057] Furthermore, the particle size of the solid material particles F can be selected according to the requirements of the reactor. For example, rapid heating is advantageous, in which case the particle size can be in the range of up to 5 mm for efficient direct heat transfer between the gas and solid phases. Therefore, short heating times of 0.1 to 1 second are possible without any problems.

[0058] Furthermore, according to one embodiment, a unimodal particle size distribution of the solid material particles F has also been found to be advantageous, as it provides uniform heating and near plug flow without uneven distribution due to partial fluidization.

[0059] The selection of electrode materials for the electrodes 20, 21 is based, inter alia, on the following criteria: Materials that are stable under the reaction conditions (temperature, gas conditions, solid-fluidized bed material) are preferred. They must have a relatively high electrical conductivity compared to the bed medium to ensure heating in the bed, not the electrode, while still allowing productivity in the required form for the entire electrode. In the simplest case, each electrode 20 is configured, for example, as a single or multiple support posts, but more complex grid configurations are also possible. In the aforementioned process, stainless steel or Ni-based alloys (due to the high temperatures) can be considered as electrode materials. For example, the material Centralloy® G 4852 Micro R is stable under reformer conditions, has acceptable strength, and can be used as an electrode material. In principle, graphite can also be used as an electrode material if steam (without steam dilution) or CO2 is not present in the feed or product gases E, P. Alternatively, graphite can be coated with a chemically stable protective layer, which must be electrically conductive.

[0060] 3, the reaction zone 12 of the reactor 1 is bounded by a peripheral wall 12a of the reactor 1, which has an inner surface 12b facing the reaction zone 12 and is of conical design, thereby providing that the reaction zone 12 tapers upward in the vertical direction z, whereby the diameter D1 of the reaction zone 12 is reduced to a diameter D2 of the reaction zone 12.

[0061] The inner surface 12b forms in particular the side of a truncated cone, in other words the reaction zone 12 forms in particular in this region a truncated cone.

[0062] Such a conically expanding shape of the reaction zone 12 advantageously results in a lateral movement of the solid material particles F of the moving bed 120 in the reaction zone 12. In the case of carbon deposits from the feed gas onto the solid material particles F, for example in the case of pyrolysis reactions (without steam) during the pyrolysis of pure methane, or in the case of coking during steam reforming when using a low steam-to-carbon ratio (also called S / C), for example S / C<1, 8, in particular S / C<1, or in the case of coking reactions during ethane cracking, bridge formation can occur, which bridges are again broken by the lateral movement of the particles F, thereby not leading to blocking.

[0063] The inner surface 12b preferably forms an angle W with the horizontal plane or cross section of the reaction zone 12, which may be relatively close to 90°.

[0064] The angle W is preferably in the range of 85° to 89.5°, and more preferably in the range of 87° to 89°.

[0065] In principle, the reactor according to the invention can be used for any other endothermic reaction, preferably without increasing solids formation in the reaction zone 12. In this regard, for example, blocking of the moving bed 120 and the associated change in bed resistance has proven to be detrimental in methane pyrolysis (CH → C + 2H).

[0066] Furthermore, it is also possible to apply an AC voltage to the resistance heater instead of a DC voltage 22 in order to heat the particles F directly by the electrodes 20,21.

[0067] The present invention advantageously makes it possible to reduce the direct CO2 emissions from the process due to the specific heating of the particles F. Furthermore, due to the heat integration between the product and the starting products in the reactor itself, no external devices for heat recovery are required, or only a reduced amount is required.

[0068] The present invention allows for relatively short heating and cooling times, resulting in good reaction control, which is particularly advantageous since rapid cooling of gases exiting the reaction zone during steam cracking is necessary to increase the yield of desired products.

[0069] Steam production can be advantageously reduced. Furthermore, no decoking cycle is necessary during ethane cracking, since the coke attached to the particles can be removed from the process. Decoking can therefore be advantageously performed outside the reactor, for example, by burning preheated air. [Explanation of symbols]

[0070] 1. Reactor 10 Inside the reactor 11 First heat integration zone 12 Reaction Zone 12a Wall 12b Inside surface 13 Second heat integration zone 20 First electrode 21 Second electrode 22 Electrical voltage or voltage source 30 Solid material particle inlet 31 Solid material particle outlet 32 Supply gas inlet 33 Supply gas outlet 110, 130 Moving floor 120 Moving Floor 330 Flow Connection F solid material particles (reactor bed) E Supply Gas P Produced gas W angle

Claims

1. A reactor (1) for carrying out an endothermic reaction, in which a product gas (P) is obtained from a feed gas (E), the reactor (1) enclosing a reactor interior (10), the reactor (1) being configured to provide a gravity-driven moving bed (120) in a reaction zone (12) of the reactor interior (10), the moving bed comprising a multitude of solid material particles (F), the reactor (1) also being configured to transfer the feed gas (E) to the reaction zone (12). ), and in order to heat the feed gas (E), the reactor (1) is configured to heat the solid material particles (F) in the reaction zone (12) by generating an electric current in the solid material particles, so that the feed gas (E) in the reaction zone (12) is heated to a reaction temperature by transferring heat from the solid material particles (F) to the feed gas (E) so that it can participate as a starting product in the endothermic reaction to produce the product gas (P), and the reactor interior (10) also comprises a first heat-integration zone (11), in which the solid material particles (F) in the reaction zone (12) are heated to a reaction temperature so that it can participate as a starting product in the endothermic reaction to produce the product gas (P), Heat from the generated product gas (P) can be transferred to the solid material particles (F) of the moving bed (120), and the reactor interior (10) also includes a second heat-integration zone (13) configured to transfer heat from the solid material particles (F) of the moving bed (120) coming from the reaction zone (12) to the feed gas (E) to preheat the feed gas (E), The reactor (1) for heating the solid material particles (F) of the moving bed (120) has a first electrode (20) and a second electrode (21), the first electrode (20) being arranged above the second electrode (21) inside the reactor (10), the reaction zone (12) is located between the first electrode (20) and the second electrode (21), the first heat-integration zone (11) is located above the first electrode (20), and the second heat-integration zone (13) is located below the second electrode; The reactor (1) has a solid material particle outlet (31), which has a control element for the moving bed velocity or mass flow rate; The feed gas (E) forms a countercurrent flow, and The reactor (1) is configured to apply a DC voltage (22) or an AC voltage between the first electrode (20) and the second electrode (21) for heating the solid material particles (F), and the first electrode (20) and the second electrode (21) comprise or are formed by a grid and further comprise one or more struts; and The reactor, characterized in that the control element is configured to control the mass flow rate of the gravity-driven moving bed (120) in the range of 0.1 to 2 m / h.

2. A reactor as described in claim 1, characterized in that the first electrode (20) and / or the second electrode (21) comprise at least one material selected from the group consisting of silicon carbide and molybdenum disilicide.

3. A reactor as described in claim 1 or 2, characterized in that the plurality of solid material particles (F) have a monomodal particle size distribution.

4. 4. The reactor according to claim 1, wherein the first electrode (20) and the second electrode (21) are in each case permeable to the solid material particles (F), the feed gas (E) and the product gas (P).

5. 4. The reactor according to claim 1, wherein the control element is a cellular wheel.

6. The reactor according to any one of claims 1 to 3, characterized in that the reactor (1) has a pair of a first electrode and a second electrode.

7. 7. The reactor (1) according to claim 1, characterized in that the reactor (1) has a solid material particle inlet (30) through which solid material particles (F) can be introduced into the first heat-integration zone (11) so that the solid material particles (F) can be led through the first electrode (20) to the reaction zone (12) and through the second electrode (21) to the second heat-integration zone (13).

8. 4. The reactor (1) according to claim 1, wherein the solid material particles (F) can be removed from the second heat-integration zone (13) through the solid material particle outlet.

9. 9. The reactor (1) according to claim 1, characterized in that it has a feed gas inlet (32) through which the feed gas (E) can be introduced into the second heat-integration zone (13) and from there through the second electrode (21) into the reaction zone (12).

10. 10. The reactor (1) according to any one of claims 1 to 9, characterized in that the reactor (1) has a product gas outlet (33) through which the product gas (P) produced in the reaction zone (12) can be removed from the first heat-integration zone (11).

11. 11. The reactor according to claim 1 , characterized in that the reactor (1) is configured to introduce the solid material particles (F) of the first heat-integration zone (11) and / or the second heat-integration zone (13) driven by gravity in the form of a moving bed (110, 130).

12. 12. The reactor according to any one of claims 1 to 11, characterized in that the reaction zone (12) of the reactor (1) is delimited by a peripheral wall (12a) of the reactor (1) having an inner surface (12b) facing the reaction zone (12) and having a conical design, so that the reaction zone (12) tapers vertically upwards.

13. 13. The reactor of claim 12, wherein the inner surface forms an angle (W) with a horizontal cross section of the reaction zone (12), the angle (W) being in the range of 85° to 89.5°.

14. A method for carrying out an endothermic reaction to obtain a product gas (P) from a feed gas (E) using the reactor according to any one of claims 1 to 13, comprising: conducting a plurality of solid material particles (F) into the first heat integration zone (11) and from the first heat integration zone into a reaction zone (12); The solid material particles (F) are heated in the reaction zone (12), conducting the solid material particles (F) from the reaction zone (12) to the second heat-integration zone (13) and removing them from the second heat-integration zone (13); the feed gas (E) is introduced into the second heat-integration zone (13) and introduced from the second heat-integration zone into the reaction zone (12); the feed gas (E) in the second heat-integration zone (13) is heated against the solid material particles (F) coming from the reaction zone (12) to cool the solid material particles (F); the feed gas (E) is brought into contact with the heated solid material particles (F) in the reaction zone (12) to transfer heat from the heated solid material particles (F) to the feed gas (E) so as to heat the feed gas (E) in the reaction zone (12); and the feed gas (E) in the reaction zone (12) is involved as a starting product in the reaction by producing the product gas (P); The generated product gas (P) is led from the reaction zone (12) to the first heat-integration zone (11), and the solid material particles (F) in the first heat-integration zone (11) are preheated relative to the product gas (P) coming from the reaction zone (12), and the product gas (P) is cooled; The product gas (P) is removed from the first heat-integration zone (11); and 3. A method according to claim 1, characterized in that the solid material particles (F) are introduced at a speed of between 0.1 m / h and 2 m / h.

15. 15. The method according to claim 14, characterized in that the flows of the heat capacity of the feed gas (E), the product gas (P) and the solid material particles (F) are matched to each other in order to recover at least 90% of the heat used.

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