REACTOR FOR ENDOTHERMAL HIGH-TEMPERATURE REACTIONS

Description

[0001] The invention relates to a reactor for endothermic high-temperature reactions, e.g. for carrying out steam reformation of a hydrocarbon-containing feed gas stream (e.g. containing methane) or e.g. for cracking or thermal splitting of ethane or e.g. for pyrolysis of natural gas (e.g. containing methane).

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

[0003] As an alternative to the established state of the art, US2,982,622 discloses, for example, a process for the production of hydrogen and high-grade coke in which inert solid particles are conveyed as bulk material in the direction of gravity through an elongated reaction zone, and an electrical voltage of 0.1 to 1000 volts per inch is applied over at least a portion of the solid mass in the reaction zone, the voltage being sufficient to raise the temperature of the solids to 1800°F to 3000°F (980°C to 1650°C). A countercurrent gas stream of hydrocarbons, preferably natural gas, is passed, which, via the endothermic pyrolysis reaction, produces hydrogen and deposits carbon on the pre-existing particles: CH4 <-> C(s) + 2 H2.

[0004] The counterflow condition of solid and gas enables heat integration, resulting in high process efficiency. By using ohmic, direct electric heating with electricity generated from renewable energy sources, the CO₂ balance of the hydrogen production process can be improved by eliminating the need for fossil fuel heating.

[0005] However, investigations have shown that the carbon deposited from the gas phase leads to a reduction in the flowability of the inert solid particles and, after prolonged operation, to a clogging of the bulk material, which significantly limits the economic viability of such a process.

[0006] Based on this, the present invention aims to provide an improved reactor that eliminates the need for fossil fuel heating of the endothermic reaction and simultaneously allows for efficient operation of the reactor.

[0007] This problem is solved by a reactor having the features of claim 1.

[0008] Advantageous embodiments of the invention are specified in the associated dependent claims and are described below.

[0009] Reactor for carrying out an endothermic reaction, in particular a high-temperature reaction, in which a product gas is obtained from a feed gas, wherein the reactor surrounds a reactor interior which is preferably divided into three zones, namely 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, wherein the moving bed consists of a plurality of solid particles which are fed in at the top end of the reactor and withdrawn at the bottom end of the reactor, wherein the reactor is further configured to guide a feed gas through the reaction zone, wherein the reactor is designed to heat the solid particles in the reaction zone (e.g. by generating an electric current in the solid particles, i.e., by generating Joule heat in the solid particles), so that the feed gas in the reaction zone can be heated to a reaction temperature by transferring heat from the solid particles to the feed gas in order to participate as a reactant in the endothermic reaction to generate the product gas, and wherein the reactor interior further comprises a first heat integration zone in which heat from the product gas generated in the reaction zone can be transferred to solid particles of the reactor bed to be introduced into the reaction zone, and wherein the interior further comprises a second heat integration zone in which heat from solid particles of the reactor bed coming from the reaction zone can be transferred to the feed gas for preheating.

[0010] According to one embodiment of the reactor, it is provided that the reactor has a first and a second electrode for heating the solid particles of the moving bed, wherein, in particular, the first electrode is arranged above the second electrode in the interior, and wherein, in particular, both electrodes are permeable to the solid particles, the feed gas, and the product gas. That is, the two electrodes are arranged or designed in such a way that the flowability of the solid particles is not impaired and the solid particles, the feed gas, and the product gas can pass through the electrodes in the reactor interior.

[0011] According to one embodiment of the reactor, the first and / or the second electrode may have one or more struts extending through the reactor interior.

[0012] Furthermore, according to one embodiment, the first electrode has a grid or is formed by a grid. The second electrode can also have a grid or be formed by a grid.

[0013] Furthermore, according to one embodiment of the invention, the first and / or the second electrode (or the respective strut or grid of the first and / or the second electrode) comprises or consists of one of the following materials: a high-temperature resistant steel, a steel alloy comprising Ni (e.g. Centralloy G 4852 Micro R), a nickel-based alloy, silicon carbide, molybdenum disilicide, graphite.

[0014] Generally, materials are preferred that are characterized by high-temperature resistance (chemical and mechanical stability at high temperatures) and the highest possible electrical conductivity. In the case of graphite, chemical stability in the presence of steam and high temperatures can be improved, for example, by a protective coating.

[0015] In one embodiment, the electrodes, the electrical supply to the electrodes, and the moving bed are also electrically insulated from the reactor pressure jacket. This is achieved, for example, by a low-conductivity, high-temperature lining, such as Al₂O₃ or ZrO₂.

[0016] Furthermore, according to one embodiment of the invention, the reactor is configured to provide or apply a DC voltage between the two electrodes for heating the solid particles.

[0017] Furthermore, according to one embodiment of the reactor, it is provided that the reactor has a solid particle inlet through which solid particles can be introduced into the first heat integration zone, so that the solid particles can be guided past the first electrode into the reaction zone and further past the second electrode into the second heat integration zone.

[0018] Furthermore, according to one embodiment of the reactor, it is provided that the reactor has a solid particle outlet through which the solid particles can be removed from the second heat integration zone, for example a rotary valve. This is the key control element for the migration speed or mass flow rate of the moving bed.

[0019] Furthermore, according to one embodiment of the reactor, the reactor has a feed gas inlet through which the feed gas can be introduced into the second heat integration zone and from there past the second electrode into the reaction zone.

[0020] Furthermore, according to one embodiment of the reactor, the reactor has a product gas outlet through which product gas generated in the reaction zone can be withdrawn from the first heat integration zone.

[0021] Furthermore, according to one embodiment of the reactor, it is provided that the reactor is configured to guide the solid particles in the first and / or the second heat integration zone by gravity in the form of a moving bed.

[0022] According to another embodiment of the reactor, the reactor is configured to guide the solid particles in the reaction zone by gravity in the form of a moving bed.

[0023] Furthermore, according to one embodiment of the reactor, the reaction zone is bounded by a circumferential wall section of the reactor, which has a conical inner surface facing the reaction zone, such that the reaction zone tapers upwards in a vertical direction. According to one embodiment, the inner surface can form an angle with a horizontal cross-section of the reaction zone, the angle preferably being in the range of 85° to 89.5°, preferably 87° to 89°.

[0024] Another aspect of the present 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, wherein a large number of solid particles are introduced into the first heat integration zone and from there into the reaction zone, the solid particles in the reaction zone are heated, the solid particles from the reaction zone are introduced into the second heat integration zone and withdrawn from the second heat integration zone, the feed gas is introduced into the second heat integration zone and from there into the reaction zone, the feed gas in the second heat integration zone is heated against solid particles coming from the reaction zone, the solid particles are cooled, and the feed gas in the reaction zone comes into contact with the heated solid particles, heat from the heated solid particles is transferred to the feed gas in the reaction zone to heat the feed gas, the feed gas in the reaction zone participates as a reactant in the reaction to generate the product gas.The generated product gas is fed from the reaction zone into the first heat integration zone, wherein the solid particles in the first heat integration zone are preheated against the product gas coming from the reaction zone, wherein the product gas is cooled, and wherein the product gas is withdrawn from the first heat integration zone.

[0025] Preferably, in one embodiment of the process, the solid particles are circulated. This means, in particular, that the solid particles removed from the second heat integration zone (possibly after intermediate treatment of the solid particles) are reintroduced into the first heat integration zone.

[0026] According to a further embodiment of the process, the feed gas is ethane (C 2 H 6 ) together with water vapor (H 2 O), which is converted in the reaction zone to ethene (C 2 H 4 ) and hydrogen (H 2 ) as product gas at temperatures preferably of about 850°C to 1250°C and pressures of 1-5 bar(a), wherein ceramic spheres, for example made of corundum (Al 2 O 3 ), are used as solid particles.

[0027] According to another embodiment of the process, the endothermic reaction is a steam reforming: CH4 + H2O -> CO + 3H2, wherein methane (CH4) is used as the feed gas together with steam (H2O) in the reaction zone (preferably at temperatures of about 950°C to 1250°C and pressures of 10 bar(a) to 100 bar(a) (preferably at pressures of 15 bar(a) to 50 bar(a)) to form carbon monoxide and hydrogen as the product gas, wherein ceramic spheres, for example made of corundum (Al2O3), are preferably used as solid particles or alternatively an abrasion-resistant Ni-based catalyst.

[0028] Furthermore, according to one embodiment, the reaction can also be a reverse water-gas shift reaction: CO 2 + H 2 -> CO + H 2 O, in which CO 2 and H 2 are reacted to form CO and H 2 O, with ceramic spheres, for example made of corundum (Al 2 O 3 ), being used as solid particles or alternatively an abrasion-resistant Ni-based catalyst.

[0029] In principle, the reaction can also be a vapor decomposition using naphtha as a feedstock.

[0030] Furthermore, according to one embodiment, the reaction can be the dehydrogenation of propane to propene (C3H8 -> C3H6 + H2), where propane is used as the feedstock and the solid particles of the reactor bed form a suitable catalyst for the reaction. Compared to a tubular fixed-bed reactor, this catalyst requires increased abrasion resistance but can advantageously be subjected to external catalyst regeneration if coking occurs during the reaction.

[0031] Furthermore, according to one embodiment, the reaction can also be a butane dehydrogenation to butene (C 4 H 10 -> C 4 H 8 + H 2 ), where butane is used as the feedstock and the solid particles of the reactor bed again form a catalyst suitable for the reaction.

[0032] Furthermore, according to one embodiment, the reaction can also be a butene dehydrogenation to butadiene (C 4 H 8 -> C 4 H 6 + H 2 ), where butene is used as the feedstock and the solid particles of the reactor bed again form a suitable catalyst for the reaction.

[0033] Furthermore, according to one embodiment, the reaction can also be an ethylbenzene dehydrogenation to styrene (C 8 H 10 -> C 8 H 8 + H 2 ), wherein ethylbenzene is used as the feedstock and, in turn, the solid particles of the reactor bed form a catalyst suitable for the reaction.

[0034] Further features and advantages of the present invention will be explained in the description of exemplary embodiments with reference to the figures. The figures show: Fig. 1 is a schematic representation of an embodiment of a reactor or a method according to the invention; Fig. 2 is a schematic representation of a further embodiment of a method according to the invention; and Fig. 3 is a schematic representation of an embodiment of a reaction zone of a reactor or a method according to the invention.

[0035] The present invention relates to a reactor 1 for carrying out an endothermic reaction, as described in the Figures 1 to 3 shown in different embodiments or applications.

[0036] Reactor 1 is designed to carry out an endothermic reaction in which a product gas P is obtained from a feed gas E. Fig. 1 Figure 1 shows a variant in which ethane is used as the feed gas E to produce ethene (C₂H₄) and hydrogen (H₂) as the product gas P. Alternatively, the reactor can be configured, for example, according to... Figure 2It can also be used for steam reforming, where methane (CH4) is used as the feed gas and reacts with steam (H2O) to produce carbon monoxide and hydrogen as the product gas P or synthesis gas. Other reactions are also conceivable.

[0037] Reactor 1 surrounds according to the Figures 1 to 3each reactor interior 10, wherein the reactor 1 is configured to provide a plurality of solid particles F in a reaction zone 12 of the reactor interior 10, the reactor 1 being further configured to introduce the feed gas E into the reaction zone 12, the reactor 1 being designed to heat the solid particles F in the reaction zone 12 so that the feed gas E in the reaction zone 12 can be heated to a reaction temperature by transferring heat from the solid particles F to the feed gas E in order to participate as a reactant in the respective endothermic reaction to generate the product gas P, and wherein the reactor interior 10 further comprising a first heat integration zone 11 in which heat from the product gas P generated in the reaction zone 12 can be transferred to solid particles F of the reactor bed 120 to be introduced into the reaction zone 12,and wherein the reactor interior 10 further comprises a second heat integration zone 13, in which heat from solid particles F of the reactor bed 120 coming from the reaction zone 12 can be transferred to the feed gas E for preheating.

[0038] In the Figure 1 and 2 In the embodiments of reactor 1 shown, the reactor bed 120 in the reaction zone 12 and the reactor beds 110, 130 in the heat integration zones are gravity-driven solid particles F, wherein the feed gas E forms a countercurrent gas flow, so that preferably almost complete heat integration can be achieved.

[0039] According to one embodiment, the heating and cooling of gases takes place on a time scale of 0.1 s to 1 s, which is advantageous for the reaction process, for example when rapid cooling to a lower temperature of the product gas is required.

[0040] As shown by the Figure 1 and 2 As can be seen, direct electrical (or inductive) heating of the solid particles F is used to heat the feed gas E. For this purpose, appropriately permeable electrodes 20, 21, in particular in the form of grids 20, 21, can be used, whereby an electrical voltage 22 is applied to the electrodes 20, 21 and thus the resistance of the solid particles F (mainly solids against solid-state contact resistances instead of material resistances) is used for heat production / heat dissipation.

[0041] To achieve optimal heat integration, the heat capacity flows of the gas and solid particle flows E, P, F are matched to each other according to a preferred embodiment. This leads to so-called heat integration zones 11, 13 in the reactor interior 10 and moving bed 110, 130, respectively, in which the feed gas E is preheated by hot solid particles F from the reaction zone 12 (lower second heat integration zone 13) and hot product gas P heats cold solid particles F that are introduced at the top of the reactor 1.

[0042] According to the Figure 1 and 2 It is preferably provided that the reaction zone 12 is arranged vertically between the two electrodes 20, 21 when the reactor 1 is arranged as intended, wherein the first heat integration zone 11 is arranged above the first electrode 20, and wherein the second heat integration zone 21 is arranged below the second electrode.

[0043] To introduce the solid particles F forming the respective reactor bed 110, 120, 130, it is further provided that the respective reactor 1 has a solid particle inlet 30, through which solid particles F can be introduced into the first heat integration zone 11, so that the solid particles F can be guided past the first electrode 20 into the reaction zone 12 and further past the second electrode 21 into the second heat integration zone 13.

[0044] To remove the solid particles F (and in particular to recirculate the solid particles F to the solid particle inlet 30), the reactor 1 also has a solid particle outlet 31, through which the solid particles F can be removed from the second heat integration zone 13.

[0045] Furthermore, each reactor 1 has a feed gas inlet 32 ​​for introducing the feed gas E into the reactor interior 10, through which the feed gas E can be introduced into the second heat integration zone 13 and from there past the second electrode 21 into the reaction zone 12.

[0046] To withdraw the product gas P, each reactor 1 has a product gas outlet 33, through which product gas P generated in the reaction zone 12 can be withdrawn from the first heat integration zone 11.

[0047] According to an example of the invention, according to Figure 1In the production of ethylene, at least 90% of the heat input is recovered, with the calculation of solid particles F based on carbon. However, ceramic materials are preferably used instead of carbon. In particular, solid particles F made of, for example, Al₂O₃ can be used as a component of the reactor bed in the present invention.

[0048] To achieve the aforementioned heat recovery, the feed gas (ethane) E can be introduced into reactor 1 at a temperature of, for example, 150°C and a pressure of, for example, 2 bar, with a mass flow rate of, for example, 1000 kg / h. The feed gas E can be diluted with steam, which has a temperature of, for example, 155°C, a pressure of, for example, 2 bar, and a mass flow rate of, for example, 300 kg / h. The conversion of ethane to ethylene can be carried out in the reaction zone at a temperature of, for example, 850°C, whereby the ethylene product can be withdrawn from reactor 1 at a temperature of, for example, 150°C, a pressure of, for example, 2 bar, and a mass flow rate of, for example, 606 kg / h. Furthermore, the solid particles F can be introduced into reactor 1 at a temperature of, for example, 174°C and a pressure of, for example, 2 bar and a mass flow rate of 2.9 t / h, and removed from reactor 1 at a temperature of 280°C.

[0049] Given a conversion rate of 65% of the input ethane to ethylene (with a steam dilution of the input with 30% water vapor), the heating power is 1550 kWh / t of ethylene product. At a 90% conversion efficiency of electrical energy, the electrical consumption is 1722 kWh / t of ethylene product.

[0050] Similar to ethane decomposition, the reactor 1 or the process according to the invention can be operated in accordance with the invention. Figure 2This can also be implemented for steam methane reforming. Instead of inert particles, a catalyst can also be used as a solid medium or solid particles F in the moving bed 110, 120, 130. Compared to a fixed-bed tube reactor, the catalyst requires increased abrasion resistance but can advantageously be subjected to external catalyst regeneration. The decision whether to use inert particles or reaction-influencing particles can be made primarily based on the reaction temperature. For example, in steam reforming, a catalyst material can be used in the lower temperature range (at approximately 950°C), while in the upper temperature range (at approximately 1250°C) the reactions proceed sufficiently quickly and an inert material can be used.

[0051] According to one embodiment, the reactor is designed to guide the solid particles through the reaction zone 12 or the heat integration zones 11, 13 at a defined speed, wherein preferably this speed of the solid particles F (e.g. in the embodiments according to Figure 1 and 2 ) in the range of 0.1m / h to 2 m / h, which is a slow and very material-friendly speed, at which the risk of friction-related damage to the reactor is correspondingly lower.

[0052] Direct electrical heating using electrodes 20, 21 at temperatures between ~800°C and -1250°C of a carbon moving bed 120 is possible with electrical resistances in the range of ~1.0 ohm to 10 ohms. For this purpose, for example, solid particles F in the form of carbon particles with a specific bed resistance of ~0.005-0.04 [ohm*m] at temperatures above 800°C can be used.

[0053] The solid particles F of the moving bed 110, 120, 130 should be sufficiently chemically stable under the reaction conditions, so that ceramic materials are preferred over carbon if the reactant gas contains steam or significant amounts of CO₂. The specific solid medium F can be selected according to the process requirements. In principle, low-resistance materials, e.g., ceramic materials, are advantageous, whereby the electrical conductivity should preferably be higher than that of the refractory lining material of the reactor 1, so that primarily the reactor bed 120 is heated and not the surrounding refractory material of the reactor. When using materials with relatively high conductivity, the contact resistance between the individual solid particles F is particularly important for the overall resistance. The surface morphology can therefore be designed to result in increased electrical resistance.According to one embodiment, the solid particles are, for example, non-spherical particles.

[0054] The length of the reaction zone 12 in the vertical direction, i.e., in the flow direction of the solid particles F and the feed gas stream E, defines the residence time of the gas in the heated zone 12. The greater the length, the more favorable the conditions for electrical heating, as this results in a correspondingly high total electrical resistance (series contact resistances of the particles F). Residence times of less than 1 s in the reaction zone 12 are possible, which is advantageous for ethylene production by ethane dehydrogenation.

[0055] Furthermore, the particle size of the solid particles F can be selected according to the reactor requirements. For example, rapid heating is advantageous for ethane dehydrogenation, where particle sizes in the range of a maximum of 5 mm ensure efficient direct heat transfer between the gas and solid phases. Short heating times of 0.1 s to 1 s are thus easily achievable.

[0056] Furthermore, according to one embodiment, a monomodal particle size distribution of the solid particles F also proves to be advantageous, since this leads to homogeneous heating and approximately to a plug flow, without segregation through partial fluidization.

[0057] The selection of the electrode material for electrodes 20, 21 is based in particular on the following criteria: a stable material under the reaction conditions (temperature, gas conditions, solid fluidized bed materials) is preferred, which exhibits a comparatively high electrical conductivity compared to the bed medium to ensure heating in the bed and not in the electrode, and the material should also allow for manufacturability in the form required for the entire electrode. In the simplest case, the respective electrode 20 is, for example, designed as a single or multiple struts, but can also have a more complex lattice structure. For the processes mentioned above, stainless steels or nickel-based alloys (due to high temperatures) can be considered as electrode materials. For example,The material Centralloy® < G 4852 Micro R is stable under reformer conditions, exhibits acceptable strength, and can be used as an electrode material. If no vapor (no vapor dilution) or CO₂ is present in the feed or product gas E, P, graphite can also be used as an electrode material. Alternatively, graphite can be coated with a chemically stable protective layer, which, however, must be electrically conductive.

[0058] Furthermore, according to a statement in the Fig. 3 In the embodiment shown, the reaction zone 12 of the reactor 1 is bounded by a circumferential wall section 12a of the reactor 1, which has an inner surface 12b facing the reaction zone 12 that is conically shaped, so that the reaction zone 12 tapers upwards in the vertical direction z. In this process, the diameter D1 of the reaction zone 12 decreases to the diameter D2 of the reaction zone 12.

[0059] The inner surface 12b forms, in particular, a lateral surface of a truncated cone. In other words, the reaction zone 12 in this area forms, in particular, a truncated cone.

[0060] Such a conically expanding geometry of the reaction zone 12 advantageously leads to a lateral movement of solid particles F of the moving bed 120 in the reaction zone 12. In the case of carbon deposits from the feed gas on the solid particles F, e.g. in a pyrolysis reaction during pure methane pyrolysis (vapor-free) or in coking during steam reforming when using small ratios of steam to carbon (also referred to as S / C), e.g. S / C< 1, 8, especially S / C<1, or in a coking reaction during ethane cracking, bridging can occur, which is broken up again by the lateral movement of the particles F and thus does not lead to blockage.

[0061] The inner side 12b preferably forms an angle W with a horizontal plane or a horizontal cross-section of the reaction zone 12, which can be relatively close to 90°.

[0062] Preferably the angle W lies in a range of 85° to 89.5°, preferably in the range of 87° to 89°.

[0063] In principle, the reactor according to the invention can be used for any other endothermic reaction, although preferably no increased solids production should occur in the reaction zone 12. In this respect, for example, in methane pyrolysis (CH4 -> C + 2H2), a blockage of the movable bed 120 and the corresponding change in the bed's resistance prove to be disadvantageous.

[0064] Furthermore, for direct heating of the particles F using the electrodes 20, 21, an alternating voltage instead of a direct voltage 22 can be applied to the resistance heater.

[0065] The present invention advantageously enables a reduced direct emission of CO2 from the process due to the specific heating of the particles F. Furthermore, the heat integration between products and reactants within the reactor itself eliminates or reduces the need for external heat recovery equipment.

[0066] The invention allows for comparatively short heating and cooling times, resulting in good reaction control. This is particularly advantageous because rapid cooling of the gas exiting the reaction zone during steam cracking is necessary to increase the yield of the target product.

[0067] Steam production can be advantageously reduced. Furthermore, decoking cycles are not necessary in ethane cracking, as coke applied to particles can be removed from the process. Therefore, decoking can be advantageously carried out outside the reactor, for example by burning off the coke in preheated air. Reference symbol list 1 reactor 10 Reactor interior 11 First heat integration zone 12 Reaction zone 12a Wall section 12b inside 13 Second heat integration zone 20 First electrode 21 Second electrode 22 Electrical voltage or voltage source 30 Solid particle inlet 31 solid particle outlet 32 Gas inlet 33 Operating gas outlet 110, 130 Moving bed 120 Moving bed 330 Flow connection F Solid particles (reactor bed) E Gas used P Product gas W angle

Claims

1. A reactor (1) for performing an endothermic reaction, in particular high-temperature reaction, wherein a product gas (P) is obtained from an input gas (E), wherein the reactor (1) encompasses a reactor interior (10), wherein the reactor (1) is configured for providing a gravity-fed moving bed (120) comprising a multiplicity of solids particles (F) in a reaction zone (12) of the reactor interior (10) so that the reactor (1) comprises a solids particle inlet (30) by means of which solids particles (F) are introducible into a first heat integration zone (11) and the reactor (1) comprises a solids particle outlet (31) comprising a control element for the speed of motion by means of which the solids particles (F) are withdrawable from a second heat integration zone (13), wherein the reactor (1) is further configured for passing the input gas (E) into the reaction zone (12) so that the input gas (E) forms a countercurrent gas stream, wherein for heating the input gas (E) the reactor (1) is configured for heating the solids particles (F) in the reaction zone (12) by generating an electric current in the solids particles so that for heating the solids particles (F) of the reactor bed (120) the reactor (1) comprises a first and a second electrode (20, 21), wherein the first electrode (20) is arranged above the second electrode (21) in the reactor interior (10), so that by transfer of heat from the solids particles (F) to the input gas (E) the input gas (E) is heatable in the reaction zone (12) to a reaction temperature allowing it to take part as a reactant in the endothermic reaction to produce the product gas (P), and wherein the reactor interior (10) further comprises a first heat integration zone (11) in which heat from the product gas (P) produced in the reaction zone (12) is transferable to solids particles (F) of the reactor bed (120) to be passed into the reaction zone (12), and wherein the reactor interior (10) further comprises a second heat integration zone (13) in which heat from solids particles (F) of the reactor bed (120) exiting the reaction zone (12) is transferable to the input gas (E) for preheating the input gas (E) so that the reaction zone (12) is arranged between the two electrodes (20, 21), wherein the first heat integration zone (11) is arranged above the first electrode (20), and wherein the second heat integration zone (13) is arranged below the second electrode.

2. The reactor according to claim 1, wherein the two electrodes (20, 21) are in each case permeable to the solids particles (F), the input gas (E) and the product gas (P).

3. The reactor according to claim 1 or 2, wherein the reactor (1) is configured for providing a direct voltage (22) or an alternating voltage (22) between the two electrodes (20, 21) for heating the solids particles (F).

4. The reactor according to any of the preceding claims, wherein the reactor (1) comprises a solids particle inlet (30) by means of which solids particles (F) are introducible into the first heat integration zone (11) so that the solids particles (F) are conductible past the first electrode (20) into the reaction zone (12) and further conductible past the second electrode (21) into the second heat integration zone (13) and the solids particles are applied at the upper end of the reactor and withdrawn at the lower end of the reactor.

5. The reactor according to any of the preceding claims, wherein the control element for the speed of motion is a rotary airlock valve.

6. The reactor according to any of the preceding claims, wherein the reactor (1) comprises an input gas inlet (32) by means of which the input gas (E) is introducible into the second heat integration zone (13) and from there conductible past the second electrode (21) into the reaction zone (12) and the reactor comprises a product gas outlet (33) by means of which product gas (P) produced in the reaction zone (12) is withdrawable from the first heat integration zone (11).

7. The reactor according to any of the preceding claims, wherein the reactor (1) is configured for conducting the solids particles (F) in the first and / or the second heat integration zone (11, 13) under gravity feed in the form of a moving bed (110, 130).

8. The reactor according to any of the preceding claims, wherein the reaction zone (12) of the reactor (1) is delimited by a circumferential wall section (12a) of the reactor (1) which has an inner surface (12b) facing the reaction zone (12) which is conical so that the reaction zone (12) narrows upwardly in the vertical direction.

9. The reactor according to claim 8, wherein the inner surface forms an angle (W) with a horizontal cross section of the reaction zone (12), wherein the angle (W) is preferably in a range from 85° to 89.5°, preferably 87° to 89°.

10. A process for performing an endothermic reaction to obtain a product gas (P) from an input gas (E) using a reactor according to any of the preceding claims, wherein - a multiplicity of solids particles (F) are passed into the first heat integration zone (11) and from there into the reaction zone (12), - the solids particles (F) are heated in the reaction zone (12), - the solids particles (F) are passed from the reaction zone (12) into the second heat integration zone (13) and are withdrawn from the second heat integration zone (13), - the input gas (E) is introduced into the second heat integration zone (13) and from there introduced into the reaction zone (12), wherein the input gas (E) in the second heat integration zone (13) is heated against solids particles (F) exiting the reaction zone (12), wherein the solids particles (F) are cooled, and wherein the input gas (E) in the reaction zone (12) is contacted with the heated solids particles (F), wherein heat from the heated solids particles (F) is transferred to the input gas (E) to heat the input gas (E) in the reaction zone (12), wherein the input gas (E) in the reaction zone (12) takes part in the reaction as a reactant to produce the product gas (P), - the produced product gas (P) is passed from the reaction zone (12) into the first heat integration zone (11), wherein the solids particles (F) in the first heat integration zone (11) are preheated against the product gas (P) exiting the reaction zone (12), wherein the product gas (P) is cooled, and wherein - the product gas (P) is withdrawn from the first heat integration zone (11).