Moving bed heater

Abstract

A heater H for electric heating of electrically conductive solid particles having a mass average particle size of ≥ 100 µm, or 50 µm to 5000 µm according to DIN 66165, comprising an inlet and an outlet for the solid particles, and wherein the heater H comprises a moving bed of said solid particles, preferably moving in the direction of gravity, the heater having the following features: i) a ratio of length l to diameter d of l / d = 1 to 100, or 0.1 to 100; ii) a voltage of 100 to 100000 V, or 10 to 1000 V; and iii) a power density of 50 to 10000 kW / m3, or 20 to 5000 kW / m3, wherein the outlet for the solid particles comprises a nonmechanical valve; a system comprising i) the inventive heater H, wherein electrically conductive solid particles are heated; ii) a reactor R1 having an inlet and an outlet for solid particles and at least one inlet and at least one outlet for gaseous components comprising a feed gas and a product gas, the reactor comprising solid particles heated in the heater; and iii) a connection between the outlet for the solid particles of the heater H and the inlet for said heated solid particles of the reactor R1; and a method comprising step i): electric heating of electrically conductive solid particles in the inventive heater H, wherein heated solid particles are obtained, wherein the electrically conductive solid particles having a descending velocity of 0.1 to 100 m / h.

Description

Moving bed heaterThe present invention relates to a heater H for electric heating of electrically conductive solid particles having a mass average particle size of > 100 m, or 50 pm to 5000 pm according to DIN 66165, comprising an inlet and an outlet for the solid particles, and wherein the heater H comprises a moving bed of said solid particles, preferably moving in the direction of gravity, the heater having the following features: i) a ratio of length I to diameter d of l / d = 1 to 100, or 0.1 to 100; ii) a voltage of 100 to 100000 V, or 10 to 1000 V; and iii) a power density of 50 to 10000 kW / m3, or 20 to 5000 kW / m3, wherein the outlet for the solid particles comprises a nonmechanical valve, a system comprising i) the heater H, wherein electrically conductive solid particles are heated; ii) a reactor R1 having an inlet and an outlet for solid particles and at least one inlet and at least one outlet for gaseous components comprising a feed gas and a product gas, the reactor comprising solid particles heated in the heater; and iii) a connection between the outlet for the solid particles of the heater H and the inlet for said heated solid particles of the reactor R1 ; and a method comprising step i): electric heating of electrically conductive solid particles in the heater H, wherein heated solid particles are obtained, wherein the electrically conductive solid particles having a descending velocity of 0.1 to 100 m / h; more preferably of 0.2 to 10 m / h, most preferably of 0.3 to 5 m / h, or 0.5 to 20 m / h, further most preferably 1 to 10 m / h, even further most preferably 4 to 10 m / h.Without electrification, the goal of climate-neutral chemistry cannot be achieved. Replacing fossil fuels with climateneutral electricity is a relevant contribution to climate neutrality. This is one reason why researchers are working intensively electrical alternatives to fossil-fuelled reactors.WO 2019 / 145279 A1 (US 20210051770 A1) relates to a heatable packed apparatus for conducting endothermic reactions which is divisible into an upper, middle and lower apparatus section, wherein the upper and lower apparatus sections are electrically insulated from the middle apparatus section, having at least one pair of electrodes in a vertical arrangement which is connected via the pressure-bearing apparatus shell in the upper and lower apparatus sections, and having an electrically conductive solid-state packing electrically insulated from the side wall of the middle apparatus section. In WO 2019 / 145279 A1, the endothermic reaction, especially a pyrolysis and the electric heating are carried out in one reactor, at the same time.One important feature of the apparatus disclosed in WO 2019 / 145279 A1 is the “thermal integration”, which “is understood to mean a countercurrent heat exchange between a hot stream of matter and a cold stream of matter in a process, the effect of which is that the sensible heat from the hot stream of matter is utilized to heat the cold stream of matter. This achieves a change in temperature of the streams of matter involved without transmission of heat flows beyond the process limits." (

[0114] in US 20210051770 A1).WO 2024 / 039872 A1 relates to a system including a pyrolysis reactor containing a bed of particulates, a solids heating section, and a separator in fluid communication with the pyrolysis reactor through the product gas outlet. The pyrolysis reactor comprises a feed gas inlet at a lower portion of the bed, a product gas outlet above the bed, a particulate outlet above the feed gas inlet, a particulate inlet near the top of the bed, and a solids product outlet in a lowerportion of the pyrolysis reactor. The solids heating section is configured to accept a portion of the particulates from the pyrolysis reactor through the particulate outlet, heat the portion of the particulates in a riser for heating solids to form heated particulates, and return the heated particulates to the pyrolysis reactor through the particulate inlet, and the separator is configured to separate any particulates in a product gas produced, and return the particulates to the pyrolysis reactor.WO 2024 / 0138017 A1 relates to a multiphase reaction process including feeding a feed stream to a first reactor to form one or more products, entraining at least a portion of the solid carbon within a gas phase product leaving the first reactor, removing a portion of the carrier particles from the first reactor as a cold carrier stream, heating the carrier particles in the cold carrier stream in a second reactor to form a heated carrier stream, passing the heated carrier stream from the second reactor to the first reactor, and providing a heat of reaction for the conversion of the feed stream to the product in the first reactor with the heated carrier stream.In WO 2024 / 039872 A1 as well as in WO 2024 / 0138017 A1 the solids are heated by using combustion or a preheated gas (e.g., an electrically heated gases, etc.).EP 0092036 A2 relates to an apparatus for heating electrically conductive bulk materials by resistive heating, comprising an inlet, an outlet and, arranged between them, end and side walls forming an oven chamber, and comprising electrodes mounted on the end walls.The purpose for the apparatus is a pre-heating of bulk material for carbon containing electrodes, e.g. in the manufacture of high grade briquettes it is known for the starting material, such as coke, soot or coal, to be intimately mixed, provided with a thermoplastic binder, particularly pitch, and then pressed. To ensure that the compression moulds are adequately filled, it is desirable for the bulk material to be preheated. The pre-heating temperatures range (according to DE 1571443 (mentioned in EP 0092036 A2, wherein no temperature is mentioned) from 150 to 250°C.US 2002 / 0007594 A1 relates to an apparatus for sustainable CO2-free production of hydrogen and carbon via continuous thermocatalytic (endothermic) decomposition of hydrocarbons over carbon-based catalyst in air and / or water- free environment, employing continuous reactivation of the catalyst, comprising the combination of:(a) a thermocatalytic reactor with a stream having a moving bed of carbon particulates;(b) means for recovering hydrogen-containing gas from said reactor;(c) means for recovering pure hydrogen from said stream;(d) means for recycling at least a portion of hydrogen-depleted gas to said reactor;(e) means for disintegration of carbon particles after said reactor; and(f) means for heating of carbon particles.It is mentioned in US 2002 / 0007594 A1 that the heat input necessary to drive the endothermic process can be provided by burning a portion of carbon with air in a heater.The reason for separating the heating of the carbon particles and the decomposition of the hydrocarbons is according to US 2002 / 0007594 A1 a complete elimination of the production of undesired contaminants, CO and CO2, in theproduction of pure hydrogen and, consequently, the need for water gas shift reaction, CO2 separation and H2 purification steps required by conventional technologies (e.g. methane steam reforming, partial oxidation, and the like).The problem of a contamination of the hydrogen by combustion products is not present in case of an electrically heated reactor as for example described in WO 2019 / 145279 A1 and WO 2024 / 039872 A1 . A separation of the use of a solid as heat carrier is therefore considered as disadvantageous in WO 2019 / 145279 A1 .However, one problem of a combined high-temperature reaction and heating in one reactor is the complexity of the reactor and the corresponding process, which - especially for upscaling - can lead to a blocking of the reactor and to uneven gas distribution and thus to less than optimal heat integration.It is therefore an object of the present invention to provide a system with less complexity, especially to reduce the problem of blocking.This object is achieved by a heater H for electric heating of electrically conductive solid particles having a mass average particle size of > 100 pm, preferably 100 pm to 1000 pm, more preferably 150 pm to 500 pm or 50 pm to 5000 pm, preferably 100 pm to 2000 pm, more preferably 100pm to 1000pm according to DIN 66165, comprising an inlet and an outlet for the solid particles, and wherein the heater H comprises a moving bed of said solid particles, moving in the direction of gravity, the heater having the following features: i) a ratio of length I to diameter d of l / d = 1 to 100, preferably 2 to 50, more preferably 5 to 25, or 0.1 to 100, preferably 0.2 to 50, more preferably 0.5 to 20; ii) a voltage of 100 to 100000 V, preferably 150 to 5000 V, more preferably 200 to 1000 V, or 10 to 1000 V, preferably 50 to 1000 V, more preferably 100 to 1000 V; and iii) a power density of 50 to 10000 kW / m3, preferably 100 to 5000 kW / m3, more preferably >200 to 2500 kW / m3, most preferably 250 to 2200 kW / m3, further most preferably 300 to 2000 kW / m3, or 20 to 5000 kW / m3, preferably 50 to 2000 kW / m3, more preferably 50 to 2000 kW / m3; wherein the outlet for the solid particles comprises a nonmechanical valve.In the heater H of the present invention no targeted chemical reaction takes place. There is therefore no "thermal integration” as described as a main feature in the apparatus disclosed in WO 2019 / 145279 A1 (US 20210051770 A1). The electrically conductive solid particles therefore generally leave the inventive heater having a very high temperature, e.g. > 800°C. Therefore, the outlet of the heater according to the present invention comprises a nonmechanical valve, which is not necessary in the apparatus disclosed in WO 2019 / 145279 A1 (US 20210051770 A1).The mass average particle size of the electrically conductive solid particles of > 100 pm, preferably 100 m to 5000 pm, more preferably 100 pm to 1000 pm, more preferably 150 pm to 500 pm, or 50 pm to 5000 pm, preferably 100 pm to 2000 pm, more preferably 100pm to 1000pm according to DIN 66165 is the particle size of fresh electricallyconductive solid particles added to the heater, before heating and / or transferring to the reactor R1 . During heating and transferring, the particle size may be reduced.The length of the reactor refers to the distance from the top of the heater to the bottom, in the direction towards the movement of the heater bed from the opening of the heater at the top to the opening of the heater at the bottom.The diameter of the heater is the largest distance between the walls of the reactor perpendicular to the movement of the reactor bed.The ratio of length I to diameter d l / d is also called “degree of slenderness”.Methods for determining the voltage (operating voltage) and the power density (volume specific power density) are known in the art.It has been found that - since no gas / solid reaction is carried out in the heater and the electrodes are completely immersed in the solid-state packing - the geometry of the reactor is independent of the need to achieve an even distribution of the reaction gas in the reactor bed. Therefore, the geometry of the heater can be chosen to obtain a uniformly heated bed with an energy consumption that is as low as necessary to heat the bed to a given temperature. The l / d ratio of the heater is generally higher than in a reactor, wherein a combined high-temperature reaction and heating in one reactor is carried out (for obtaining the same uniformly heated bed). Further, the power density of the heater is generally high, and therefore a compact design of the heater is achieved.The inventive heater has for example the following advantages:~ The CO2 emissions of the process are eliminated if electrical energy from renewable sources is used in the moving bed heater.- The degree of utilization of the energy input is increased, as the proportion that is lost in the state of the art with the flue gas stream of the burner is saved. This results in a chain of of successive advantageous properties: the solids flow can be thermally efficiently heated to a much higher temperature level compared to the state of the art. The required throughput (flow rate) of the circulating solid to transfer a given thermal power is significantly reduced compared to the state of the art.- The abrasion of the particles and the wear of the lining are significantly reduced compared to the state of the art. The high temperature level achieved in the moving-bed heater enables an extended range of applications for heating fluidized bed reactors with solid heat carriers.It should be considered that especially the power density, which is desired to be as high as possible in the sense of a design as compact as possible, is limited in a reactor, wherein a combined high-temperature reaction and heating in one reactor is carried out. E.g., in methane pyrolysis, the power density is generally limited.Preferably, the inventive heater comprises at least one, preferably all of the following features:iv) a specific resistance of the electrically conductive solid particles (i.e. the fill) of 1 .00E-5 to 1 Ohm*m, preferably 1.00E-4 to 0.1 Ohm*m, more preferably 5.00E-4 to 0.01 Ohm*m, or 0.001 to 0.1 Ohm*m, preferably 0.002 to 0.05 Ohm*m, more preferably 0.005 to 0.02 Ohm*m; v) an amperage of 100 to 150000 A, preferably 1000 to 100000 A, more preferably 2000 to 50000 A, or 100 to 500000 A, preferably 500 to 300000 A, more preferably 1000 to 100000 A; vi) a heat output of 100 to 500000 kW, preferably 1000 to 100000 kW, more preferably 5000 to 50000 kW, or 10 to 200000 kW, preferably 50 to 100000 kW, more preferably 100 to 50000 kW; vii) a current density of 1000 to 100000 kA / m2, preferably 2000 to 75000 kA / m2, 2500 to 50000 kA / m2, or 500 to 20000 A / m2, preferably 1000 to 20000 A / m2, more preferably 1000 to 10000 A / m2.The specific resistance depends on the nature of the electrically conductive solid particles. Examples for suitable electrically conductive particles are mentioned below. The specific resistance is generally determined as known in the art, for example by the quadripole method: This is a widely used method for measuring the resistivity of materials. Current is fed at two points, and the voltage drop is measured between two other points. The resistivity can then be calculated using Ohm's law and the geometry of the sample.The amperage generally depends on the heat output and the specific resistance of the electrically conductive solid particles. The amperage is generally determined as known in the art.The heat output is generally determined as known in the art.The current density results from the power density and the specific resistance of the electrically conductive solid particles.More preferably, the inventive heater comprises at least one, preferably all of the following features: A cross-sectional area of 0.01 to 50 m2, preferably 0.05 to 30 m2, more preferably 0.1 to 10 m2; A heated length of 1 to 100 m, preferably 1 to 60 m, more preferably 1 to 40 m;A field strength of 5 to 500 V / m, preferably 10 to 250 V / m, more preferably 20 to 250 V / m;A mass flow of 20 to 200000 kg / h, preferably 50 to 100000 kg / h, more preferably 100 to 50000 kg / h;A cross-sectional load of 0.1 to 20 kg / m2 / s, 0.1 to 10 kg / m2 / s, 0.1 to 5 kg / m2 / s, preferably 0.2 to 3 kg / m2 / s, more preferably 0.3 to 2 kg / m2 / s;A person skilled in the art knows how the features mentioned above are determined.Suitable inlets for the electrically conductive solid particles introduced at the top of the heater are known in the art.The inlet is generally an opening for feeding solid material particles. Upstream and fluidically connected with the inlet may be a feed chamber serving as reservoir for solid material particles to be introduced. In a preferred embodiment,upstream and fluidical ly connected with the inlet or optionally with the feed chamber, a rotary valve or a screw conveyor is installed, allowing controlled introduction of the solid material particles into the heater. The electrically conductive solid particles may be introduced into the heater having a very high temperature, e.g. > 600°C. Materials and means for handling the hot solids (especially > 600°C) are known in the art and mentioned below.Since no targeted chemical reaction takes place in the inventive heater, the heater preferably does not comprise an inlet for a gaseous reactant.In a further embodiment, the heater does not comprise an inlet for a gaseous feed at the bottom of the heater, preferably, the heater comprises exactly one opening ant the bottom, which is the outlet for the solid particles, i.e., the heater has an opening for the solids flow at the lower, hot end and otherwise has a closed, lined shell.In the meaning of the present invention, a reactant is a starting material that participates in chemical reactions leading to the formation of desired products. Specifically, in hydrocarbon pyrolysis, the reactants are typically hydrocarbons. During pyrolysis, these hydrocarbons are subjected to high temperatures in the absence of oxygen, causing them to break down into smaller molecules, such as alkenes, alkynes, and other valuable products. In methane pyrolysis, for example, the reactant is methane or a methane comprising gas and the desired products are hydrogen and carbon.Suitable outlets for the electrically conductive solid particles leaving the heater at the bottom are known in the art. The outlet may be for example a chute. At the end of the outlet, generally a discharge valve is installed. Suitable discharge valves are rotary vales or screw conveyors, preferably rotary valves. This allows controlled removal of the solid material particles from the heater. The electrically conductive solid particles may leave the heater having a very high temperature, e.g. > 800°C. Materials and means for handling the hot solids (especially > 800°C) are known in the art and mentioned below.The electrically conductive solid particles preferably having a velocity (descending velocity) of 0.1 to 100 m / h; more preferably of 0.2 to 10 m / h, most preferably of 0.3 to 5 m / h, or 0.5 to 20 m / h, further most preferably 1 to 10 m / h, even further most preferably 4 to 10 m / h. Since no targeted chemical reaction takes place in the inventive heater, the descending velocity can be higher than in an apparatus, wherein a heating (e.g. of solid particles) and a reaction (e.g. hydrocarbon pyrolysis) are carried out.In the presence of a gaseous feed, the upward gas flow limits the descending velocity of the solid material, due to the following interdependence: The gas flow rate determines the solid's descending solid velocity in order to achieve efficient heat recovery. This gas flow rate is constrained by the fluidization threshold, which in turn restricts the solid flow rate.Materials for the heater for handling the hot solids are known in the art. In "The Moving Bed Fuel Reactor Process”, Andrew Tong, Mandar V. Kathe, Dawei Wang, and Liang-Shih Fan, Handbook of Chemical Looping Technology,First Edition. Edited by Ronald W. Breault. © 2019 Wiley-VCH Verlag GmbH & Co. KGaA. Published 2019 by Wiley- VCH Verlag GmbH & Co. KGaA, especially chapter 1.3.2 „Heat Management", for example, an attractive alternative to mechanical valves for solids flow control is the use of nonmechanical solids flow control devices. These devices refer to valves with no internal mechanical moving parts and that only use aeration gases in conjunction with their shape to manipulate the solid particles flow through them. The nonmechanical solids flow control devices have no moving parts and thus have no issues of wear and tear, especially under extreme operating conditions such as elevated temperatures and pressures. Also, these devices are normally inexpensive as they are constructed from ordinary pipes and fittings. Due to their simplicity, the nonmechanical solids flow control devices can be quickly fabricated avoiding the long delivery times associated with mechanical valves. They are widely used in industries due to their advantages over mechanical solids flow control devices. The most common types of nonmechanical solids flow control devices, also called nonmechanical valves, include the L-valve and J-vaive. Further suitable L-valves and non-mechanical valves are described in US 2017 / 0130148 A1 and the literature mentioned therein.The outlet for the solid particles of the inventive heater H therefore comprises a nonmechanical valve, preferably an L-valve or a J-valve. Suitable nonmechanicai valves, e.g. L-vaives and J-valves are known in the art, as for example mentioned above.In the moving bed of electrically conductive solid particles of the inventive heater, the solid particles preferably move through the heater under the influence of gravity. In the heater according to the present invention, the moving bed is preferably operated continuously and / or discontinuously.In a continuous moving bed heater, solid particles flow continuously through the reactor without interruption. Key features generally include:■ Constant flow: Particles are continuously fed at the top and discharged at the bottom, maintaining a steady flow; or continuous discharge: Particles are continuously discharged at the bottom; the feed may be introduced continuously or discontinuously.■ Steady-state operation: The reactor can maintain consistent conditions over long periods, making it suitable for large-scale industrial processes.■ Flow patterns: The particle flow can be characterized by different modes, including continuous discharging and intermittent discharging (synchronous or asynchronous).A discontinuous moving bed operates in cycles rather than continuously. Key features generally include:■ Intermittent operation: The bed moves in discrete steps or cycles rather than continuously, and preferably, the heating power varies.■ Batch-like process: While not a true batch process, it shares some characteristics with batch operations.■ Control over residence time: The intermittent nature allows for more precise control over the time particles spend in different heater zones.■ Flexibility: This type can be more adaptable to heating that require varying treatment times or conditions for different batches of material.According to the present invention, no hydrocarbon feed for carrying out a targeted reaction is added to the heater, especially, no targeted chemical reaction is carried out in the heater.Therefore, preferably, no significant amounts of gas are present in the heater and the amount of gas leaving the heater is 0 to 500 Vol% / h, based on the total volume of the bed of solid particles.In a further preferred embodiment, the amount of gaseous hydrocarbon entering the bed, preferably the amount of gas entering the bed is 0-10 Vol%, preferably 0 to 5 Vol%, based on the total volume of the bed.One feature of the heater is that the electrically conductive solid particles are introduced into the heater at the top having a temperature lower than the temperature of the electrically conductive solid particles leaving the reactor at the bottom.The electrically conductive solid particles are introduced into the heater, generally having a temperature of 10 to 1800°C, preferably 500 to 1500 °C.In the heater, the solid particles are generally heated to a temperature of 300 to 2000 °C, preferably 600 to 1800 °C, more preferably > 800 to 1800 °C, most preferably 900 to 1600°C, i.e. the electrically conductive solid particles leaving the heater, generally having a temperature of 300 to 2000 °C, preferably 600 to 1800 °C, more preferably > 800 to 1800 °C, most preferably 900 to 1600°C.A temperature increase (AT) in the inventive heater is generally 100 to 1000K, preferably 100 to 700K, more preferably 100 to 500K.The temperature in the heater is determined as known in the art, e.g. by direct temperature measurement using one or more known temperature sensors. For example, thermocouples can be used as temperature sensors. A practical design for technical use are sheath-thermocouples, such as those described in the prior art in DE 10 2019 111 882 B4. However, the installation of sheath-thermocouples in a moving bed heater generally requires the installation of one or more protective sleeves in the heater. The protective sleeves have various functions: They form the channel for the measuring lines to pass through the heater wall. They must be mechanically robust, for example to withstand the forces imposed by the moving bed material. They must also form a gas-tight and, if necessary, pressure-resistant barrier between the interior of the heater and the ambient. Furthermore, the protective sleeves must be electrically insulating. In order to meet these requirements, the cross-section of the protective sleeves must be chosen accordingly. This results in two problems: the precision of the measurement can be impaired and the uniformity of the solid flow can be disturbed. This can result in local overheating of the solid-state packing. Another problem is associated with the bushing of the protective sleeve through the heater wall. The heater wail usually consists of several layers of different materials. Large temperature differences can occur between the layers. These inevitably result from the need to thermally insulate the interior of the heater from the environment. As a result, the layers of the wail tend toexpand thermally to different extents. In order to prevent a collision of some layer of the heater wall with the protective sleeve, a recess should be cut out that is significantly larger than the cross-section of the protective sleeve. However, this can impair the function of the heater wall.However, the temperature in the heater, especially the final temperature at the lower end, can be in addition or as alternative to the direct temperature measurement known in the art derived from the ohmic resistance.The ohmic resistance can be derived from the operating parameters of the current input current and voltage between the electrodes via Ohm's law. From the ohmic resistance, the temperature in the heater according to the invention, in particular the final temperature at the lower end, can be determined by means of a suitable calibration. This value can be used as a virtual temperature sensor. This has the following advantages over direct temperature measurement using an ordinary temperature sensor:- The measurement is integral, i.e. it records the complete volume of the heating section. Based on this measurement, a suitable model can be used to render the distribution of the temperature in the heating zone with high temporal and spatial resolution. This allows possible disturbances and irregularities in the heating of the moving bed to be detected.- A uniform flow of solids over the cross-section of the heater is ensured, which is not hindered by internals such as protective sleeves of temperature sensors.The use of electric energy as a heat source instead of for example heating by combustion of natural gas allows considerable advantages, in particular regarding the ease of control. The use of electricity offers opportunities for the use of compact, modular, high performance and energy efficient heaters. When the electricity derives from a non-fossil resource, the heater can be operated without net emission of carbon dioxide.The electric heating of the heater according to the present invention may be any electric heating known in the art. The heater may be configured comprising a directly contacted bed (direct heating) and / or an inductively heated bed (inductive heating). Another option is a heat input through electromagnetic waves (radio or microwaves). Preferably, the electric heating is direct and / or inductive heating, more preferably direct heating, wherein most preferably at least one pair of electrodes is at least partially in electrically conductive connection with the solid particles, preferably, at least one pair of electrodes is fully in electrically conductive connection with the solid particles.Generally, the terms “direct heating” and “inductive heating” are known by a person skilled in the art.The different heating concepts of supplying heat may be combined. For example, the thermal energy generated by passing the current through the electrically conductive bed may be supplemented by other heat sources.In the preferred variant of resistive heating with a directly contacted bed, a voltage is applied across at least a portion of the bed to generate an electric current through the respective portion of the bed. The electric current is generally conducted through a plurality of electrodes (two or more) that are in an electrically conductive relationship with thebed, e.g., immersed in a randomly packed particle bed or electrically connected to a structured packed bed, preferably completely immersed in a randomly packed particle bed. Especially said preferred embodiment allows the level in the heater to be varied over a wide range and can form a conical upper surface without affecting the function of the heater.The electrodes may be made of a metal, graphite or any other suitably conductive material. Preferably, the electrodes are made of at least one metal of one or more of the groups 5, 6 and 11 of the IUPAC Periodic Table of the Elements or alloys comprising at least one metal of one or more of the groups 5, 6 and 11 of the I UPAC Periodic T a- ble of the Elements, a graphite-containing material, stainless steel, or mixtures thereof, preferably molybdenum, a molybdenum containing alloy, niobium, a niobium containing alloy, tungsten, a tungsten containing alloy, copper, a copper containing alloy, a graphite-containing material, stainless steel, or mixtures thereof.Preferably, a pair of axially spaced electrodes is employed, i.e., upper and lower electrodes. Alternatively, a radial electrode arrangement may be contemplated with a central electrode extending along the axis of the heater and a generally cylindric counter electrode or a pair of concentric cylindrical electrodes with a cylindrical inner electrode and a cylindrical outer electrode so that an electric current is induced with radially oriented streamlines between the electrodes.The shape of the electrodes is not particularly limited. Preferably, the electrodes are designed to achieve a uniform current distribution within the particle bed. Preferably, the electrodes take the shape of a grid or of rods. Suitable electrode assemblies are described in WO 2019 / 145279 A1.When rods are used, each electrode preferably comprises several rods distributed across the cross section of the particle bed. Electrode rods that run to a point are particularly advantageous. Preferably, the upper and lower electrode rods run to a point on the side toward the heated zone. The tip may be conical or wedge-shaped. Correspondingly, the end of the rod may take the form of a dot or a line. The rod electrodes are connected to the hood in an electrically conductive manner and are jointly supplied with electrical power via the hood.Preferably, the electrodes take the form of a grid. For grid form, various configuration variants are conceivable, for example grids in honeycomb form composed of advantageously regular polygons, rectangular grids formed from parallel bars, grids in the form of spokes or grids composed of concentric rings. Particular preference is given to grids in the form of spokes and grids composed of concentric rings.The potential or voltage may arise from an A.C. or D.C. source. A potential difference (voltage) of 100 volt to 10 000 V, preferably 150 to 5000 V, more preferably 200 to 1000 V, or of 10 to 1000 V, preferably 50 to 1000 V, more preferably 100 to 1000V is applied.This advantageously results in an electric current density in the bed of 1000 to 100000 kA / m2, preferably 2000 to 75000 kA / m2, 2500 to 50000 kA / m2, or of 500 to 20000 A / m2, preferably 1000 to 20000 A / m2, more preferably 1000 to 10000 A / m2.According to the invention, in the preferred resistive heating with a directly contacted bed, an electric current can flow through the electrically conductive solid particles forming the moving bed. When the bed is a structured packed bed, the material of the structure of the packing can be intrinsically electrically conductive, or the structure can be coated with an electrically conductive coating.In a particle bed, the particles comprise electrically conductive solid particles through which an electric current flows. The particle bed must contain a sufficient proportion of electrically conductive particles to ensure macroscopic electrical conductivity of the particle bed and allow for the passage of an electrical current through the bed. The proportion of electrically conductive particles in the particle bed can be in the range of 5% and 100%, preferably of 20% and 100 %, most preferably of 50 and 100% by volume, further most preferably of 80 to 100% by volume, based on the total volume of the electrically conductive solid particles.The electrically conductive solid particles generally having a specific resistance of 1 .00E-5 to 1 Ohm*m, preferably 1.00E-4 to 0.1 Ohm*m, more preferably 5.00E-4 to 0.01 Ohm*m, or of 1.00E-7 to 0.1 OhmTn, preferably 5.00E-7 to 0.05 OhmTn, more preferably 1.00E-6 to 0.01 OhmTn.Preferably, the heating in the heater according to the present invention is a direct heating and the specific resistance of the electrically conductive solid particles forming the moving bed is 1.00E-5 to 1 OhmTn, preferably 1.00E-4 to 0.1 OhmTn, more preferably 5.00E-4 to 0.01 OhmTn, or of 0.001 to 0.1 OhmTn, preferably 0.002 to 0.05 OhmTn, more preferably 0.005 to 0.02 OhmTn.The electrically conductive solid particles present in the heater may be of any kind as long as the particle size is as mentioned above. Preferably, the electrically conductive solid particles having a specific resistance of 1 .00E-5 to 1 OhmTn, preferably 1.00E-4 to 0.1 OhmTn, more preferably 5.00E-4 to 0.01 OhmTn, or of 0.001 to 0.1 OhmTn, preferably 0.002 to 0.05 OhmTn, more preferably 0.005 to 0.02 OhmTn.Preferably, the electrically conductive solid particles present in the heater having a specific heat capacity of 250 to 2500 J / kg / K, preferably 400 to 2000 J / kg / K, more preferably 400 to 2000 J / kg / K.Preferably, the electrically conductive solid particles present in the heater having a bulk density of 200 to 3000 kg / m3, preferably 500 to 2000 kg / m3, more preferably 500 to 2000 kg / m3.The electrically conductive solid particles may comprise or consist of a material which is inherently conductive or of a material which may be rendered conductive by the reactive deposition of an electrically conducting material, e.g., carbon.In one embodiment, the particle bed contains chemically active particles. Chemically active particles include catalytically active particles, reactants of a chemical conversion or carriers for deposition of products of the chemical conversion. Catalytically active particles exert a catalytic activity on the chemical conversion. The chemically active particlesmay be reactants or products of a chemical conversion, particularly in a moving bed method outside the heater (e.g. in a reactor R1 as mentioned below).The electrically conductive particles themselves may be chemically active or may be essentially catalytically inert. The electrically conductive particles may be admixed with non-conductive particles. The non-conductive particles may be chemically active particles.Suitably, the electrically conductive solid particles are electrically conductive particles and preferably comprise at least one carbonaceous material, one or more metals, ceramic, silicon carbide particles, or a mixture thereof, preferably a carbonaceous material, preferably comprising at least 50 wt% of carbon, more preferably having a carbon content of 98 wt% to 100 wt%, based on the total amount of the carbonaceous material.The plurality of solid material particles may be in the form of fines, or be agglomerated such as pelletized or granulated, if required, as long as the mass average particle size of > 100 m, or 50 pm to 5000 pm according to DIN 66165.In another embodiment, the plurality of solid material particles is selected from adsorbents and absorbents, such as superabsorbent polymers, comprising varying degrees of moisture.Preferred carbonaceous material is a macro-structured carbonaceous material, more preferably a macro-structured carbonaceous material having a porosity in the range of 30 to 70 vol%, based on the total volume of the carbonaceous material.Suitable carbonaceous material may include particles of char or coke, in particular graphite particles. Suitable metals (metal particles) may be metallic throughout or have a metallic coating over a non-metallic core. Metallic particles include conductive pre-reduced oxidic particles.The present invention further relates to a method comprising: i) electric heating of electrically conductive solid particles in a heater H according to the present invention, wherein heated solid particles are obtained, wherein the electrically conductive solid particles having a descending velocity of 0.1 to 100 m / h; preferably of 0.2 to 10 m / h, more preferably of 0.3 to 5 m / h, or 0.5 to 20 m / h, further most preferably 1 to 10 m / h, even further most preferably 4 to 10 m / h.In the presence of a gaseous feed, the upward gas flow limits the descending velocity of the solid material, due to the following interdependence: The gas flow rate determines the solid's descending solid velocity in order to achieve efficient heat recovery. This gas flow rate is constrained by the fluidization threshold, which in turn restricts the solid flow rate.Preferred embodiments and parameters of step i) are mentioned above, especially regarding the description of the heater. Preferably, no hydrocarbon feed is added into the heater.In a further preferred embodiment, step i) does not comprise a targeted chemical reaction.According to the present invention, the heated electrically conductive solid particles obtained in the heater may be used in reactions, wherein heated solid particles are involved. Said reactions are carried out according to the present invention in an apparatus different from the heater, for example in a reactor R1, which is preferably connected with the heater for a transfer of the heated electrically conductive solid particles. However, in case that the heated solid particles are calcined, said calcination can be carried out directly in the heater, e.g. in case of petroleum coke as heated solid particles. Petroleum coke is a carbon-rich solid material derived from oil refining. It is generally a byproduct of the coking process, where heavy fractions of crude oil are heated to high temperatures to break them down into lighter products. Petroleum coke can be used as a fuel or in industrial applications, such as in the production of aluminum or steel.Petroleum coke can be further processed into calcined petroleum coke by heating it to remove volatile materials and increase its carbon content. Calcination typically occurs at temperatures of fer example 1200 to 1350°C. This process enhances the coke's properties, making it suitable for use in applications that require high purity and conductivity, such as in the anodes of aluminum smelters.The present invention therefore further relates to a system comprisingI) A heater H for electric heating of electrically conductive solid particles having a mass average particle size of> 100 m, or 50 pm to 5000 pm according to DIN 66165, comprising an inlet and an outlet for the solid particles, and wherein the heater H comprises a moving bed of said solid particles, preferably moving in the direction of gravity, the heater having the following features: i) a ratio of length I to diameter d of l / d = 1 to 100, preferably 1 to 50, more preferably 1 to 20, or 0.1 to 100, preferably 0.2 to 50, more preferably 0.5 to 20; ii) a voltage of 10 to 100000 V, preferably 50 to 100000 V, more preferably 100 to 100000 V, or 10 to 1000, preferably 50 to 1000, more preferably 100 to 1000; and iii) a power density of 50 to 10000 kW / m3, or 20 to 5000 kW / m3, preferably 50 to 2000 kW / m3, more preferably 50 to 2000 kW / m3; preferably a heater according the present invention as defined above, wherein electrically conductive solid particles are heated;II) A reactor R1 having an inlet and an outlet for solid particles and at least one inlet and at least one outlet for gaseous components comprising a feed gas and a product gas, the reactor comprising solid particles heated in the heater; andIII) A connection between the outlet for the solid particles of the heater H and the inlet for said heated solid particles of the reactor R1 .The heater is described above. Suitable reactors R1 are known by a person skilled in the art. Preferably, the reactor R1 is a reactor for carrying out a high-temperature reaction, preferably an endothermic reaction, in which more preferably the product gas is obtained e.g. from gas-phase reactions or from gas-solid reactions. More preferably, the reactor R1 is a fluidized bed reactor, a spouting bed reactor or a moving bed reactor. More preferably, the reactor isconfigured to provide a moving bed or a fluidized bed (moving bed or fluidized bed reactor), preferably a gravity- driven moving bed, which moving bed or fluidized bed comprises said solid particles heated in the heater.The heated solid particles can serve to transfer heat into the reactor R1 to allow a reaction to occur. Suitable reactions are high-temperature reactions, preferably endothermic reactions. Examples for suitable reactions are mentioned below. The use of the heated solid particles can allow heat to be introduced into the reactor R1 without the use of additional heating elements being present within the reactor R1 itself.It is, however, also possible that the reactor R1 comprises one or more additional heating elements. Suitable additional heating elements are known in the art and for example mentioned in the documents mentioned below or mentioned in the description of the heater above. Suitable reactors R1 are known in the art and for example described in WO 2019 / 145279 A1, WO 2024 / 039872 A1, WO 2024 / 138014 A1, US 2002 / 0007594 A1. If a heating system is present, an electric heating system is preferred.Preferably, the feed gas moves in a counterflow to the solid particles.More preferably, the reactor R1 is a moving bed reactor (R), wherein a product gas is obtained from a feed gas, the reactor having a top (T) and a bottom (B), wherein the reactor comprises: an inlet (IS) for introducing the hot electrically conductive solid particles of the heater H at the top and for passing the electrically conductive solid particles through the reactor in the direction of gravity, an inlet (IG) for introducing a feed gas at the bottom and for ascending of the feed gas from there into the reaction zone, wherein in a reaction zone, the feed gas is contacted with the solid material particles and participates as a starting product in the reaction of producing the product gas, and the product gas ascends in direction of the top of the reactor, counter-currentiy to the electrically conductive solid particles, wherein the feed gas is heated by the solid material particles moving towards it, an outlet (OG) for leaving of the product gas at the top of the reactor, and an outlet (OS) for leaving of the electrically conductive solid particles at the bottom of the reactor.In a further preferred embodiment, the reactor R1 is a fluidized bed reactor, wherein a product gas is obtained from a feed gas, the reactor having a top (T) and a bottom (B), wherein the reactor comprises: an inlet (IS) for introducing the hot electrically conductive solid particles of the heater H, typically at the bottom of the reactor; these particles are fluidized by the upward flow of the feed gas; an inlet (IG) for introducing the feed gas at the bottom of the reactor; the velocity of the feed gas is adjusted to fluidize the solid particles, creating a fluid-like state where the particles are suspended and well-mixed within the gas; whereinin a reaction zone, the feed gas is contacted with the fluidized solid material particles, and the feed gas participates as a starting product in the reaction to produce the product gas; the product gas, optionally along with any entrained solid particles, ascends towards the top of the reactor; an outlet (OG) is located at the top of the reactor for the exit of the product gas; cyclones and / or filters may be used to separate any entrained solid particles from the product gas before it exits the reactor; an outlet (OS) for removing excess solid particles or for recycling them at least in part back into the system, typically located at the bottom of the reactor.According to the present invention, the term "bottom” of the reactor generally covers the bottom itself and the lower section of the reactor (preferably the lower 25% in relation to the total length of the reactor). The term "top” of the reactor generally covers the top itself and the upper section of the reactor (preferably the upper 25% in relation to the total length of the reactor).The outlet (OS) for leaving of the electrically conductive solid particles at the bottom of the reactor is preferably connected with the inlet of the heater. By this step, heated recycled electrically conductive solid particles are obtained at the solid particle outlet of the heater.As mentioned above, electrically conductive solid particles heated in the heater are in a preferred method of the present invention introduced into the reactor R1 . Said heated electrically conductive solid particles may be fresh electrically conductive solid particles (i.e. solid particles which have not been used in a reaction in the reactor R1 before) and / or recycled electrically conductive solid particles. Preferably, a mixture of fresh and recycled electrically conductive solid particles are introduced into the reactor R1. In case that a mixture is used, the recycled electrically conductive solid particles obtained in the heater can be mixed with fresh electrically conductive solid particles which have also been heated in the heater or with fresh solid particles which have not been heated in the heater before. Preferably, both, the recycled electrically conductive solid particles and the fresh electrically conductive solid particles have been heated in the heater before. Usually, the recycled electrically conductive solid particles and the fresh electrically conductive solid particles are heated together in said heater before introduction into the reactor R1.Therefore, the electrically conductive solid particles added to the heater are the electrically conductive solid particles leaving the reactor R1, fresh electrically conductive solid particles or a mixture of both.Suitable inlets for the plurality of solid particles introduced, preferably at the top of the reactor are known in the art and are generally the same as mentioned for the heater. Since the solid material introduced into the reactor R1 has a high temperature, high temperature resistant materials are used for the solids inlet of the reactor R1 . Suitable materials are mentioned above.Suitable outlets for the plurality of solid material particles leaving the reactor at the bottom are known in the art and are generally the same as mentioned for the heater. However, the temperature of the solids at the outlet, preferably at the bottom of the reactor R1 is typically lower than at the inlet. Therefore, it is not in every case necessary to employ high temperature resistance material.Suitable inlets for introducing the feed gas, preferably at the bottom of the reactor are known in the art. In one embodiment, the feed gas is introduced into the reactor via a gas distribution chamber being located at the bottom of the reactor and generally having a perforated floor.Suitable outlets for withdrawing the product gas, preferably at the top of the reactor are known in the art.In the system according to the present invention, the electrically conductive solid particles are preferably recirculated. That is to say, in particular, that the electrically conductive solid particles withdrawn from the reactor R1 (possibly after an intermediate treatment of the solid material particles) are returned to the heater.However, a part of the solid particles leaving the reactor R1 is generally discharged from the reactor R1 . The part (fraction) of solid particles discharged is then replaced by the addition of the appropriate amount of fresh electrically conductive solid particles to the heater. The electrically conductive solid particles can for example be discharged continuously or in a semi-batch or batch process.Generally, the solid particles are introduced into the reactor R1 with a temperature of 300 to 2000 °C, preferably 600 to 1800 °C, more preferably > 800 to 1800 °C, most preferably 900 to 1600°C. The temperature may be lower than the temperature of the solids leaving the heater, e.g. 0 to 5°C lower.The term "high-temperature processes” encompasses pyrolysis reactions, dehydrogenation reactions, reforming reactions inter alia.According to the invention, the endothermic high-temperature process is preferably a process wherein the volumespecific energy consumption in the heated zone, also called reaction chamber, is greater than 0.5 MW / m3, more preferably greater than 1 MW / m3, especially greater than 2 MW / m3. For example, the energy consumption may be between 0.5 and 10 MW / m3in the heated zone. However, lower values are also generally possible.The reaction according to the present invention may be selected from chemical conversions such as dehydrations and dehydrogenations; and physical transformations such as drying operations. Reactors in which physical transformations are performed may also referred to as vessels. The terms "vessel” and "reactor” are thus used interchangeably herein without, however, necessarily implying a limitation to chemical conversions.The present invention may be applied to a wide variety of chemical reactions. The chemical reaction may simply involve the decomposition of a reactant, but may also involve other reactants, in particular other gaseous reactants or solid reactants such as particles constituting the particle bed.In preferred embodiments, the chemical conversion is selected from(I) Gasification of solid feedstocks (coal, heavy residues), also known as cokingCxHy+ H2O (x-y)C(s) + zCO + (z+y / 2)H2in a fluidized-bed of coke particles(ii) Hydrocarbon pyrolysis, especially methane pyrolysis according to the idealized equationCH4^ C + 2 H2over a bed of carbon particles;(ill) Cracking of hydrocarbons according to the idealized equationC(n+m)H(2n+2m+2) * CnH(2n)+CmH(2m)+H2 over a bed of carbon;(iv) reforming of ammonia according to the idealized equation2 NH3— > N2+ 3H2over a bed of particles of transition metal (such as Fe or Ni) supported on a refractory support material;(v) decomposition of methanol according to the idealized equationCH3OH — > CO + 2 H2over a bed of Cu catalyst;(vi) reforming of methanol according to the idealized equationCH3OH + H2O — > CO2+ 3 H2over a bed of Cu catalyst;(vii) Reverse Water Gas Shift Reaction according to the idealized equationCO2+ H2CO + H2O over a bed of Ni catalyst;(viii) Methane Steam Reforming according to the idealized equationCH4 + H2O ^ CO + 3 H2over a bed of SIC, C, Ni catalyst or Fe catalyst;(ix) Methane Dry Reforming according to the idealized equationCH4+ CO22 CO + 2 H2over a bed of SIC, C, Ni catalyst or Fe catalyst;(x) formation of hydrocyanic acid by the reaction of ammonia with hydrocarbons according to the idealized equationCH4+ NH3^ HCN + 3 H2over a bed of carbon particles;(xi) formation of hydrocyanic acid by formamide cleavage according to the idealized equationHCONH2^ HCN + H2O over a bed of stain less particles or Fe catalyst;(xii) Boudouard reaction according to the idealized equationC02+ C — > 2 00 over a bed of carbon particles;(xiii) dehydroaromatization of methane according to the idealized equation6 CH4C6H6+ 9 H2over a bed of Mo catalyst, optionally a mixed bed of Mo catalyst and carbon particles;(xiv) alkane dehydrogenation according to the idealized equationCnH(2n+2) -> CnH(2n) + H2, wherein n = 2,3,4 over a bed of FeO / Pt catalyst, optionally over a mixed bed of FeO / Pt catalyst and carbon particles;(xv) styrene synthesis according to the idealized equationCsHio — > CsHs + H2 over a bed of FeO / Pt catalyst, optionally over a mixed bed of FeO / Pt catalyst and carbon particles;(xvi) formation of anhydrous formaldehyde according to the idealized equationCH3OH CH20 + H2over a bed of Ag catalyst;(xvii) cyclohexane dehydrogenation according to the idealized equationC6Hl2 ^ C6H6 + 3 H2over a bed of Pt catalyst;(xviii) alcohol dehydration according to the idealized equationCnH(2n+i)OH — > CnH(2n) + H2O, wherein n = 2,3,4 over a bed of zeolith catalyst, optionally including carbon particles;(xix) vinyl formamide synthesis from cyanoethyl formamide according to the idealized equationCH3CH(CN)(NH-COH) CH2CH(NH-COH) + HCN over a mixed bed of potassium hydroxide on alumina and carbon particles, or carbonized catalyst of potassium hydroxide on alumina;(xx) melamine synthesis according to the idealized equation6 (NH2)2CO C3N6H6 + 6 NH3+ 3 CO2over a mixed bed of bauxite and carbon particles, or carbonized bauxite;(xxi) oxidation of sulfur dioxide to sulfur trioxide as first step in the production of sulfuric acid, according to equation2SO2+ O22SO3over a bed of vanadium(V) oxide catalyst;(xxii) calcination of catalysts by decomposition of, e.g., nitrates, carbonates and hydroxides;(xxiii) drying of granulates in agricultural, wood and food industries; in paper, animal feed and pellet production; or in cement and recycling industry;(xxiv) regeneration of adsorbents, e.g., activated carbon; and(xxv) regeneration of carbonized catalysts, e.g., desulfurization catalysts like Mo-Co on gamma-alumina, MTO catalysts and styrene catalysts.Preferred examples of applications are:(i) Gasification of solid feedstocks (coal, heavy residues), also known as cokingCxHy+ H2O (x-y)C(s) + zCO + (z+y / 2)H2in a fluidized-bed of coke particles(ii) Hydrocarbon pyrolysis, especially methane pyrolysis according to the idealized equation CH4 ^ C + 2 H2over a bed of carbon particles, preferably at temperatures from 1200°C to 1500°C;(viii) Methane Steam Reforming according to the idealized equationCH4 + H2O ^ CO + 3 H2over a bed of SiC, C, Ni catalyst or Fe catalyst, preferably C (carbon particles), preferably at temperatures from 1000°C to 1300°C;(ix) Methane Dry Reforming according to the idealized equationCH4 + CO2^ 2 CO + 2 H2over a bed of SiC, C, Ni catalyst or Fe catalyst; , preferably C (carbon particles), preferably at temperatures from 1000°C to 1300°C;(x) formation of hydrocyanic acid by the reaction of ammonia with hydrocarbons according to the idealized equation CH4 + NH3^ HCN + 3 H2over a bed of carbon particles, preferably at temperatures from 1400°C to 1500°C.Preferably, the chemical conversion is conversion (ii) and (iii). Especially preferred is chemical conversion (i).According to the present invention, the temperature in the reaction zone of the reactor R1 is generally 500 to 2000°C, preferably 800 to 1600°C, more preferably 1000 to 1500°C. The pressure in the reactor is generally 1 to 100 bar, preferably 5 to 50 bar.A particularly preferred embodiment of the invention relates to a hydrocarbon pyrolysis process carried out in the reactor R1. Suitable and preferred hydrocarbons are mentioned above. Hydrocarbon pyrolysis is a technology that splits hydrocarbons, especially aliphatic hydrocarbons such as methane, ethane, propane and / or butane directly into hydrogen and solid carbon. Most often, natural gas comprising methane is used as feedstock for methane pyrolysis. For methane, the pyrolysis proceeds according to the following main reaction:CH4^ C + 2 H2The process is moderately endothermic (standard reaction enthalpy: 74.91 kJ / mol of CH4). It is evident from the reaction equation above that in hydrocarbon pyrolysis, the release of greenhouse gases is prevented. Therefore, in the event that the electric energy originates from renewable resources, hydrocarbon pyrolysis is a CO2-free, i.e. , clean technology to obtain emission-free hydrogen. It is also possible to use a non-fossil hydrocarbon feedstock like biomethane. Hydrocarbon pyrolysis is a one-step process which produces hydrogen in high volume.As the energy demand of the hydrocarbon pyrolysis contributes to the energy-penalty of the carbon fixture, a hydrocarbon pyrolysis process having an as high as possible energy efficiency is preferred. Moving carbon bed hydrocarbon pyrolysis is preferred due to several aspects, such as higher hydrogen yields. More preferred is a hydrocarbon pyrolysis in a fluidized bed reactor.The obtained solid carbon can be sold as a commercial product for selected applications, depending on the carbon morphology and physical / chemical properties. For example, the solid carbon from hydrocarbon pyrolysis may beused for aluminum and steel production, tire manufacturing, electrode manufacturing, polymer blending, additive for construction materials, carbon devices like heat exchangers, soil conditioning, or storage.Carbon particles act as the electrically conductive particles and as substrate for the deposition of carbon generated by the decomposition of the hydrocarbon compounds. The carbon particles can either be porous or non-porous and can be a granular or powder-like material. The particle size of a preferred support substrate is - in case of a moving carbon bed hydrocarbon pyrolysis - in the range of 0.3 to 20 mm, preferably 0.5 to 15 mm, more preferably 1 to 10 mm. The particle size of a preferred support substrate is - in case of a fluidized carbon bed hydrocarbon pyrolysis - in the range of 50 m to 5000 pm, preferably 100 pm to 2000 pm, more preferably 100pm to 1000pm.Suitable reaction temperatures are mentioned above. The pyrolysis is preferably carried out at temperatures ranging from 700 to 2000°C. The pressure preferably ranges from 1 to 100 bar.A preferred pyrolysis method comprises the steps of: a) pyrolysis of hydrocarbons over a moving bed or fluidized of carbonaceous particulates in the reactor R1 , preferably carbon particles, whereby carbon is deposited on the surface of the carbonaceous particulates; p) recovering a stream of hydrogen-containing gas; y) directing the stream of hydrogen-containing gas to a gas separation unit to obtain pure hydrogen and hydrogen- depleted gas;5) recirculating the hydrogen-depleted gas to the reactor R1;E) withdrawing carbon particles at the bottom of the reactor R1 ; and optionallyQ classifying the withdrawn carbon particles, preferably via sieving; q) discharging a fraction of withdrawn carbon particles as a product;9) recirculating a fraction of withdrawn carbon particles directly to the heater.A stream of a hydrocarbon feedstock enters the reactor R1 where it is thermocatalytically decomposed (pyrolyzed) over the moving bed of the carbonaceous particles.Preferably, according to the present invention, the product gas comprises hydrogen (Fh-product), preferably 10 to 100 vol%, more preferably 15 to 85 vol% hydrogen (H2-product) based on the total volume of the product gas. The hydrogen-containing raw product gas may pass a gas-solid separation unit as described in the following. A filter, a cyclone, or any other system capable of separating fine particles from a gas stream, may be employed as the gassolid separation unit. The purified gas stream is optionally directed through a heat exchanger and further to a gas separation unit. A gas separation membrane, a pressure swing adsorption (PSA) system, a cryogenic absorption (or adsorption) unit, or any other system capable of separating hydrogen from hydrocarbons, may be employed as the gas separation unit. A stream of pure hydrogen is separated from the gaseous stream. A hydrogen-depleted gas is preferably recirculated to the reactor R1.The system according to the present invention comprises means for heat recovery from gaseous components leaving the reactor R1 and / or from solid particles leaving the reactor R1 .Generally, means for heat recovery from gaseous components leaving the reactor R1 and / or from solid particles leaving the reactor R1 are known in the art and for example described in Werther, J. (2000). Fluidized-bed reactors. Ullmann's encyclopedia of industrial chemistry, WO 2019 / 145279 A1 , WO 2024 / 039872 A1 , WO 2024 / 138017 A1 , US 2002 / 0007594 A1.Examples for means for heat recovery from the solid particles leaving the reactor R1 comprise a reactor R2a for preheating the feed gas; a reactor R2b for generating steam which is preferably used for heating and / or process applications or to drive turbines, or combinations thereof.Examples for means for heat recovery from the gaseous components leaving the reactor R1 comprise means for generating steam which is preferably used for heating and / or process applications or to drive turbines; means for reintroducing a part of the gaseous components into the reactor R1 and / or R2a, or combinations thereof. Especially, a hydrogen-depleted gas is preferably recirculated to the reactor R1 and / or R2a, as described above. For example, a pressure swing absorption (PSA) unit can be used to separate the hydrogen from the remaining components. The hydrogen-depleted gas can be recycled the reactor R1 and / or R2a.The present invention further relates to a method comprising i) Electric heating of electrically conductive solid particles in a heater H as described in the present application, wherein heated solid particles are obtained; ii) Transferring the heated solid particles to a reactor R1 , having an inlet and an outlet for said solid particles and at least one inlet and at least one outlet for gaseous components comprising a feed gas and a product gas, preferably via a connection between the outlet for the solid particles of the heater H and the inlet for said heated solid particles of the reactor R1 ; wherein the electrically conductive solid particles having in step i) a descending velocity of 0.1 to 100 m / h; preferably of 0.2 to 10 m / h, more preferably of 0.3 to 5 m / h, or 0.5 to 20 m / h, further most preferably 1 to 10 m / h, even further most preferably 4 to 10 m / h.Step i) of the inventive method has already been described above.Preferably, the cross-sectional load in the inventive method is 0.1 to 20 kg / m2 / s , 0.1 to 10 kg / m2 / s, 0.1 to 5 kg / m2 / s, preferably 0.2 to 3 kg / m2 / s, more preferably 0.3 to 2 kg / m2 / s.Preferred embodiments and parameters of step ii) are mentioned above, especially regarding the description of the reactor R1 .More preferably, the method according to the present invention comprises in addition to step i) and step ii) step iii)Reaction of a feed gas in the presence of the heated solid particles in the reactor R1 for obtaining a product gas, wherein the reaction is preferably an endothermic reaction, more preferably a high-temperature reaction, in which the product gas is obtained from the feed gas, most preferably a gasification or a pyrolysis.Preferred embodiments and parameters of step iii) are mentioned above, especially regarding the description of the reactor R1 .The method according to the present invention comprises one or more steps for heat recovery from gaseous components leaving the reactor R1 and / or from solid particles leaving the reactor R1 .Suitable steps for heat recovery from gaseous components and solid particles are known in the art and for example described in Werther, J. (2000). Fluidized-bed reactors. Ullmann's encyclopedia of industrial chemistry, WO 2019 / 145279 A1, WO 2024 / 039872 A1, WO 2024 / 138014 A1, US 2002 / 0007594 A1 and mentioned above.Preferably, the inventive method is carried out in a system according to the present invention.The invention is exemplified in the following figures and examples.The abbreviations (functional identification) mentioned in the circles in Fig. 1 to 5 are part of the standardized notation in process engineering (DIN e.V. (Ed.) (DIN 19 2278 part 1): DIN 19 2278 part 1, „Graphische Symbole und Kennbuchstaben fur die ProzeBleittechnik", Beuth-Verlag, Berlin, 1993) and have the following meanings:For symbols comprised on a circle, the top letters are the functional indicator, the bottom numbers are the measurement on control value and the following suffix indicated whether there are multiple instruments in a chain.The functional identification consists of a first letter, designating the measured or initiating variable (examples include F-flow, P-pressure, T-temperature, L-levei). In the case of FV, the first letter F stands for flow. The second (and sometimes third and fourth letters) are modifiers.Common abbreviations are:TC: Temperature sensor and temperature controllerFC: Flow regulator or flow controllerLC: Level ControllerEC: Electrical quantities controller (controlling the power input)ER: Electrical value register (monitoring the electrical conductivity of the solid-state packing)LCAS: Level Control, Alarm and ShiftingTIA: Temperature indication and AlarmQC: Quality controllerFigure 1 presents the block diagram of a general embodiment of the process of the invention.In figures 2 to 5 preferred embodiments of the present invention are exemplified (without limiting the full scope of the patent application):Figure 2 shows an example for a schematic representation of the heater 10 according to the invention and preferred measuring and control circuits.The numbers in Fig. 2 have the following meanings:10 heater H, e.g. a shaft-shaped apparatus11 a, b two electrodes, preferably vertically arranged12 power source, preferably direct current (DC)13 ohmic resistance recording, optional14 upper inlet15 outlet (discharge)17 packing of electrically conductive solid particles, preferably carbonaceous particlesExample 1The operation of the inventive heater is shown by the following example 1:The heater in Fig. 2 is preferably a shaft-shaped apparatus. The heater is filled with a packing of carbonaceous particles 17. The carbonaceous particles have a weight average grain size of 0.3 mm. The bulk density is 980 kg / m3. The heat capacity of the carbonaceous particles is 1980 J / (kg K). The purpose of the heater according to the invention is in the present example to conduct a stream of solids from these particles with a throughput of 50,000 kg / h from top to bottom and thereby to heat it from the inlet temperature of 1000 °C to the outlet temperature of 1500 °C. For this purpose, the device has a cross-section of 7 m2and two vertically arranged electrodes 11 a, b at a vertical distance of 16.5 m from each other. The electrodes are embedded in the packing. The electrodes are connected to a DC source 12. The electric current with a current of 20.9 kA is conducted into the bulk via the electrodes. The packing has an electrical resistance of 31 .5 mQ. The heating capacity is 13.75 MW. There is a voltage of 658 V between the electrodes.Solids are supplied via the upper inlet 14. The fill level in the heater is controlled by the particle flow rate in inlet 14. The setpoint of the level is 1000 mm above the upper electrode. The level of the packing next to the wall is used as a measure of the fill level. Via discharge 15 at the lower end of the device, the solids flow rate through the heating zone is controlled.Optionally, the ohmic resistance 13 of the packing between the electrodes is measured. As explained above, from the ohmic resistance, the temperature in the heater according to the invention, in particular the final temperature at the lower end, can be determined by means of a suitable calibration. This value can be used as a virtual temperature sensor for controlling the outlet temperature of the stream of solids.Figure 3 shows a more specific design of the heater according to Figure 2.The numbers in Fig, 3 have the following meanings:10 heater H, e.g, a shaft-shaped apparatus11 a, b two electrodes, preferably vertically arranged12 power source, preferably direct current (DC)13 ohmic resistance, optional14 upper inlet15 outlet (discharge)17 packing of electrically conductive solid particles, preferably carbonaceous particles21 reservoir (feeder)22 fluidization gas flow25 seal pot32 conveyed gas flow36 L-valveExample 2The operation of an exemplified design of the inventive heater is shown by the following example 2:The goods to be treated are fed from feeder 21 into the process line via line 24. The solids flow serves as the manipulated variable for the fill level control in the moving bed heater. The fill level control is designed as a two-point control. When the level reaches the lowest limit, solids are conveyed from reservoir 21 , The conveyance of the solids is interrupted as soon as the fill level reaches the highest limit. A seal pot 25 is used for dosing the product. The solids flow rate is controlled by the fluidization gas flow 22, Solids conveying starts as soon as the fluidization flow is activated and stops as soon as the fluidization flow is interrupted. Nitrogen is used as the fluidizing gas. The rules for the design of the sealing pot are known to the skilled person, for example Yang, W. C. (2003), Handbook of fluidization and fluid-particle systems. CRC press. The throughput of the solids stream is not measured directly. Rather, it is controlled by a characteristic curve that relates the throughput of the solid material to the flow rate of the fluidizing gas flow 22. In the specific example, the fluidization flow is 550 Nm3 / h.The treated solids flow is discharged at the lower end of the process route via an L-vaive. The rules for the design of the L-valve are known to the skilled person, for example Yang, W. C. (2003). Handbook of fluidization and fluid-particle systems. CRC press. The cross-section of the L-valve is 0.11 m2. The target value for the conveyed gas flow is 15 Nm3 / h. The throughput of the solids flow 15 is continuously regulated. The throughput of the solids flow is not measured directly. Rather, it is controlled by a characteristic curve that relates the throughput of the solid material to be conveyed to the throughput of the conveyed gas flow 32. The regulator output acts on the flow rate of the conveyed gas flow 32. The solids flow rate is controlled by the flow rate of the conveying gas flow 32.Figure 4 shows a more specific design of the heater according to Figure 2.The numbers in Fig. 4 have the following meanings:10 heater H, e.g. a shaft-shaped apparatus11a,b two electrodes, preferably vertically arranged12 power source, preferably direct current (DC)13 ohmic resistance, optional14 upper inlet15 outlet (discharge)17 packing of electrically conductive solid particles, preferably carbonaceous particles21 reservoir (feeder)22 fluidization gas flow25 seal pot42 conveyed gas flow 4243 fluidizing gas46 J-valveExample 3Figure 4 shows a more specific design of the heater according to Figure 2. The goods to be treated are fed from feeder 21 into the process line via line 24. The solids flow serves as the manipulated variable for the fill level control in the moving bed heater. The fill level control is designed as a two-point control. When the level reaches the lowest limit, solids are conveyed from reservoir 21 . The conveyance of the solids is interrupted as soon as the fill level reaches the highest limit. A seal pot 25 is used for dosing the product. The solids flow rate is controlled by the fluidization gas flow 22. Solids conveying starts as soon as the fluidization flow is activated and stops as soon as the fluidization flow is interrupted. Nitrogen is used as the fluidizing gas. The rules for the design of the sealing pot are known to the skilled person, for example Yang, W. C. (2003). Handbook of fluidization and fluid-particle systems. CRC press. The throughput of the solids stream is not measured directly. Rather, it is controlled by a characteristic curve that relates the throughput of the solid material to the flow rate of the fluidizing gas flow 22. In the specific example, the fluidization flow is 550 Nm3 / h.The treated solids flow is discharged at the lower end of the process route via a J-valve. The rules for the design of the J-valve are known to the skilled person, for example Yang, W. C. (2003). Handbook of fluidization and fluid-particle systems. CRC press. The cross-section of the L-valve is 0.11 m2. The throughput of the solids flow 15 is continuously controlled. The throughput of the solids stream is not measured directly. Rather, it is controlled by a characteristic curve that relates the throughput of the solid material to be conveyed to the throughput of the conveyed gas flow 42. The regulator output acts on the flow rate of the conveyed gas flow 42. The solids flow rate is controlled by the flow rate of the conveying gas flow 42. The target value for the conveyed gas flow is 15 Nm3 / h.In addition, a fluidizing gas 43 is introduced into the upward branch in order to equalize the flow rate of the solid. The setpoint of the fluidization gas flow is 45 Nm3 / h.Figure 5 shows an application of the apparatus according to the invention.The numbers in Fig. 5 have the following meanings:10 heater H, e.g. a shaft-shaped apparatus12 power source, preferably direct current (DC)14 upper inlet of the heater15 outlet (discharge)19 make-up solids inlet IS50 fluidized bed gasifier R51 inlet for fluidizing gas55 feeding line (for feeding a (partial) flow of petroleum coke)59 residue feed60 classifier61 steam flowExample 4Figure 5 shows an application of the apparatus according to the invention. The moving bed heater 10 is used as a heating section for the heat supply of a fluidized bed coking plant. The fluidized bed gasifier 50 is designed according to the state of the art, for example based on the Exxon Fluid Coking process. The reactor processes heavy-boiling residues of oil refinement, which are fed into the reactor via inlet 59. Steam is used as a fluidizing gas and enters the reactor via inlet 51 . The calcined coke is discharged via the classifier 60. The steam flow 61 serves as a quench gas and fluidizing gas for the transport of the solid product stream. The gasification reaction is supplied with heat by feeding a partial flow 55 of the petroleum coke from the fluidized bed gasifier to the moving-bed heater. Optionally, a make-up stream of solid particles 19 can be added. In the moving-bed heater the particles are heated and returned to the fluidized bed gasifier via side flow 15. The moving bed heater replaces the burner in which part of the solid is burned with air to generate the required process heat.The following advantages result from the use of the device according to the invention:• The yield of calcined coke is increased• The CO2 emissions of the process are eliminated if electrical energy from renewable sources is used in the moving bed heater.• The degree of utilization of the energy used is increased, as the proportion that is lost in the state of the art with the exhaust gas flow of the burner is saved. This results in a chain of advantageous properties: the solids flow can be thermally efficiently heated to a much higher temperature level compared to the state of the art. The required throughput of the circulating solid to transfer a given thermal power is significantly reduced compared to the state of the art.• The abrasion of the particles and the wear of the lining are significantly reduced compared to the state of the art.• The high temperature level achieved in the moving-bed heater results in an extended range of applications for heating fluidized bed reactors with solid heat transfer fluids. Examples of applications are mentioned above.

Claims

Claims1 . A heater H (10) for electric heating of electrically conductive solid particles (17) having a mass average particle size of > 100 m, or 50 pm to 5000 pm according to DIN 66165, comprising an inlet (14) and an outlet (15) for the solid particles, and wherein the heater H (10) comprises a moving bed of said solid particles, preferably moving in the direction of gravity, the heater having the following features: i) a ratio of length I to diameter d of l / d = 1 to 100, preferably 1 to 50, more preferably 1 to 20, or 0.1 to 100, preferably 0.2 to 50, more preferably 0.5 to 20; ii) a voltage of 10 to 100000 V, preferably 50 to 100000 V, more preferably 100 to 100000 V, or 10 to 1000, preferably 50 to 1000, more preferably 100 to 1000; and iii) a power density of 50 to 10000 kW / m3, or 20 to 5000 kW / m3, preferably 50 to 2000 kW / m3, more preferably 50 to 2000 kW / m3; wherein the outlet for the solid particles comprises a nonmechanical valve.

2. The heater according to claim 1, wherein the nonmechanical valve is a L-valve (36) or a J-valve (46).

3. The heater (10) according to claim 1 or 2, wherein the moving bed is operated continuously and discontinuously.

4. The heater (10) according to any one of claims 1 to 3, wherein an amount of 0-10 Vol%, preferably 0 to 5 Vol% based on the total volume of the bed, of gaseous hydrocarbon, preferably of gas is entering the bed.

5. The heater (10) according to any one of claims 1 to 4, wherein the heater does not comprise an inlet for a gaseous reactant.

6. The heater (10) according to any one of claims 1 to 5, wherein the temperature at the top of the heater is 100 to 1900 K, preferably 150 to 1500 K lower than the temperature at the bottom of the heater.

7. The heater (10) according to any one of claims 1 to 6, wherein the electric current is directly conducted or inductively coupled in the bed of said solid particles.

8. The heater (10) according to any one of claims 1 to 7, wherein the solid particles comprise at least one carbonaceous material, one or more metals, ceramic, silicon carbide particles, or a mixture thereof, preferably a carbonaceous material, preferably comprising at least 50 wt% of carbon, more preferably having a carbon content of 98 wt% to 100 wt%, based on the total amount of the carbonaceous material.

9. The heater (10) according to any one of claims 1 to 8, wherein the solid particles are heated to a temperature of 300 to 2000 °C, preferably 600 to 1800 °C, more preferably 900 to 1600°C.

10. The heater (10) according to any one of claims 1 to 9, wherein the heater comprises at least one, preferably all of the following features: iv) a specific resistance of the electrically conductive solid particles (i.e. the fill) of 1 .00E-5 to 1 Ohm*m, preferably 1.00E-4 to 0.1 OhmTn, more preferably 5.00E-4 to 0.01 OhmTn, or 0.001 to 0.1 OhmTn, preferably 0.002 to 0.05 OhmTn, more preferably 0.005 to 0.02 OhmTn; v) an amperage of 100 to 150000 A, preferably 1000 to 100000 A, more preferably 2000 to 50000 A, or 100 to 500000 A, preferably 500 to 300000 A, more preferably 1000 to 100000 A; vi) a heat output of 100 to 500000 kW, preferably 1000 to 100000 kW, more preferably 5000 to 50000 kW, or 10 to 200000 kW, preferably 50 to 100000 kW, more preferably 100 to 50000 kW; vii) a current density of 1000 to 100000 kA / m2, preferably 2000 to 75000 kA / m2, 2500 to 50000 kA / m2, or 500 to 20000 A / m2, preferably 1000 to 20000 A / m2, more preferably 1000 to 10000 A / m2.

11. The heater (10) according to any one of claims 1 to 10, wherein the heater comprises: ii) a voltage of 100 to 1000 V.

12. The heater (10) according to any one of claims 1 to 11, wherein the heater comprises the following features: i) a ratio of length I to diameter d of l / d = 0.5 to 20; ii) a voltage of 100 to 1000 V; and iii) a power density of 50 to 2000 kW / m3.

13. The heater (10) according to claim 12, wherein the heater comprises the following features: iv) a specific resistance of the electrically conductive solid particles (i.e. the fill) of 0.005 to 0.02 OhmTn; v) an amperage of 1000 to 100000 A; vi) a heat output of 100 to 50000 kW; vii) a current density of 1000 to 10000 A / m2.

14. The heater (10) according to any one of claims 1 to 13, wherein the cross-sectional load is 0.1 to 20 kg / m2 / s , 0.1 to 10 kg / m2 / s, 0.1 to 5 kg / m2 / s, preferably 0.2 to 3 kg / m2 / s, more preferably 0.3 to 2 kg / m2 / s.

15. A method comprising: electric heating of electrically conductive solid particles in a heater H according to any one of claims 1 to 14, wherein heated solid particles are obtained, wherein the electrically conductive solid particles having a descending velocity of 0.1 to 100 m / h; more preferably of 0.2 to 10 m / h, most preferably of 0.3 to 5 m / h, or 0.5 to 20 m / h, further most preferably 1 to 10 m / h, even further most preferably 4 to 10 m / h h.

16. A system comprisingI) A heater H (10) for electric heating of electrically conductive solid particles having a mass average particle size of > 100 m, or 50 pm to 5000 pm according to DIN 66165, comprising an inlet (14) and an outlet for the solid particles, and wherein the heater H (10) comprises a moving bed of said solid particles, preferably moving in the direction of gravity, the heater having the following features: i) a ratio of length I to diameter d of l / d = 1 to 100, preferably 1 to 50, more preferably 1 to 20, or 0.1 to 100, preferably 0.2 to 50, more preferably 0.5 to 20; ii) a voltage of 10 to 100000 V, preferably 50 to 100000 V, more preferably 100 to 100000 V, or 10 to 1000, preferably 50 to 1000, more preferably 100 to 1000; and iii) a power density of 50 to 10000 kW / m3, or 20 to 5000 kW / m3, preferably 50 to 2000 kW / m3, more preferably 50 to 2000 kW / m3; preferably a heater (10) according to any one of claims 1 to 13, wherein electrically conductive solid particles are heated;II) A reactor R1 (50) having an inlet (19) and an outlet for solid particles and at least one inlet (51) and at least one outlet for gaseous components comprising a feed gas and a product gas, the reactor comprising solid particles heated in the heater; andIII) A connection between the outlet for the solid particles of the heater H and the inlet for said heated solid particles of the reactor R1 .

17. The system according to claim 16, wherein the reactor R1 (50) is a reactor for carrying out a high-temperature reaction, preferably an endothermic reaction, in which the product gas is obtained from the feed gas, wherein the reactor is configured to provide a moving bed or a fluidized bed, preferably a gravity-driven moving bed, which moving bed or fluidized bed comprises said solid particles heated in the heater.

18. The method according to claim 15, additionally comprising step ii): ii) Transferring the heated solid particles to a reactor R1 (50), having an inlet and an outlet for said solid particles and at least one inlet and at least one outlet for gaseous components comprising a feed gas and a product gas, preferably via a connection between the outlet for the solid particles of the heater H (10) and the inlet for said heated solid particles of the reactor R1 (50).

19. The method according to claim 16, additionally comprising the step iii) iii) Reaction of a feed gas in the presence of the heated solid particles in the reactor R1 (50) for obtaining a product gas, wherein the reaction is preferably an endothermic reaction, more preferably a high-tem- perature reaction, in which the product gas is obtained from the feed gas, most preferably a pyrolysis.

20. The method according to claim 18 or 19, which is carried out in a system according to claim 16 or 17.

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