Reactor for carrying out exothermic reactions, as well as use and methods for operating such a reactor

Abstract

The present invention relates to a reactor (1) for carrying out exothermic reactions comprising a plate heat exchanger (2) with a plurality of adjacent plates (3) between which gap channels (4, 5) are defined, wherein the gap channels (4, 5) are divided into several fluidically interconnected primary gap channels (4) and several fluidically interconnected secondary gap channels (5), wherein a catalyst material (6) for an exothermic reaction is provided in at least one of the primary gap channels (4), and wherein primary fluid supply means (7) for supplying a primary fluid to the primary gap channels (4) and secondary fluid supply means (10) for supplying a secondary fluid to the secondary gap channels (5) are provided, a pressure vessel (18) surrounding the plate heat exchanger (2), and pressure fluid supply means (19) configured to supply a pressure fluid to the pressure vessel (18).

Description

[0001] The invention relates to a reactor for conducting exothermic reactions. Furthermore, the invention relates to the use and a method for operating such a reactor.

[0002] The applicant is aware that different designs are used for heat transfer devices. The purpose of such devices is to transfer heat from a hot side (heat source) to a cold side (heat sink). In the simplest case, heat sources and sinks can be heat transfer fluids, such as water (steam) or thermal oil.

[0003] Specifically, heat sinks can be endothermic reactions, and heat sources can be exothermic reactions. Special heat sinks are catalyzed, endothermic reactions. The applicant is aware that the following reactor types are sometimes used for such reactions: - Heated tube bundle reactors - Adiabatic beds with intermediate heating (tray reactor) - Heated fluidized bed reactors

[0004] Plate reactors are also known from the prior art. These offer the advantage of a large exchange surface. However, due to their rectangular shape, they are only partially pressure-resistant.

[0005] Chemical reactions, such as endothermic reactions, often occur at elevated pressure, which can pose significant challenges to the reactors used. Examples of endothermic reactions that occur at elevated pressure, including reactor types used to the applicant's knowledge, are: - Ammonia cracking - Tray and tube bundle reactor - Methane steam reforming - Tube bundle reactor - Methanol steam reforming - Tube bundle reactor - Propane and butane dehydrogenation (Oleflex) - Tray reactor

[0006] All of the aforementioned reactor concepts have disadvantages. In adiabatic beds with intermediate cooling, the catalyst beds are usually very large, as the catalyst is not efficiently utilized. Furthermore, a comparatively large amount of equipment is required for the intermediate heat exchangers. While heated tube-bundle reactors have comparatively good catalyst utilization, they are generally very expensive because they scale based on the number of tubes.

[0007] In the field of electrolysis and fuel cell technology, electrolysis and fuel cell stacks arranged in a pressure vessel are known. A high-pressure electrolysis cell, for example, is described in JP 5 524 227 B2.

[0008] US 6 153 083 A discloses an electrolyzer for electrolyzing water into hydrogen and oxygen, comprising a number of electrolysis cells, each containing an anode and a cathode, which are connected in series in a cell block surrounded by a pressure vessel.

[0009] US 6 689 499 B2 discloses pressurized fuel cell generator modules protected by purge gas.

[0010] JP 3 845 780 B2 discloses atmospheric and pressurized SOFC power generation systems.

[0011] US 4,259,312 A discloses a method and apparatus for the catalytic reaction of a reducing gas and water vapor. The apparatus comprises a pressure vessel in which several catalyst beds and heat exchangers are arranged, alternating.

[0012] DE 601 29 686 T2 discloses a reactor for exothermic or endothermic heterogeneous reactions. The reactor comprises a pressure vessel in which several heat exchangers are arranged, embedded in a catalytic layer.

[0013] It is therefore an object of the present invention to provide an alternative reactor for conducting exothermic reactions, which avoids or at least reduces the aforementioned disadvantages and can be manufactured with comparatively little effort. It is also an object of the invention to provide a method for operating such a reactor.

[0014] The first-mentioned object is achieved according to the invention by a reactor for carrying out exothermic reactions comprising - a plate heat exchanger with a plurality of adjacent plates, in particular at least substantially parallel to one another, between which gap channels are defined, wherein the gap channels are divided into a plurality of fluidically interconnected, in particular fluidically parallel, primary gap channels, and a plurality of fluidically interconnected, in particular fluidically parallel, secondary gap channels, wherein in at least one of the primary gap channels, preferably in all primary gap channels, a catalyst material for an exothermic reaction, in particular for a catalytic oxidation reaction, preferably for a catalytic oxidation reaction of hydrogen, particularly preferably a catalytic combustion of hydrogen with oxygen, is provided,and wherein primary fluid supply means are provided for supplying a primary fluid to the primary gap channels and secondary fluid supply means are provided for supplying a secondary fluid to the secondary gap channels, - a pressure vessel surrounding the plate heat exchanger, - Pressure fluid supply means designed to supply a pressure fluid to the pressure vessel and in particular to generate an increased pressure of at least 2 bar, in particular of at least 5 bar, preferably of at least 10 bar, particularly preferably of at least 20 bar in the pressure vessel.

[0015] The second object is achieved according to the invention by a method for operating a reactor according to the invention, comprising the steps - a primary fluid is supplied to at least one primary gap channel, preferably to all primary gap channels, and an exothermic reaction, in particular an oxidation reaction of hydrogen, preferably a catalytic combustion of hydrogen with oxygen, is carried out in the at least one primary gap channel, preferably in all primary gap channels, - a secondary fluid is supplied to at least one secondary gap channel, preferably to all secondary gap channels, - a pressure fluid, in particular a pressure gas, is preferably supplied to the pressure vessel, wherein the pressure fluid N 2 and / or comprises or is given by liquid water and / or water vapor and / or air.

[0016] In other words, the present invention proposes the use of a plate heat exchanger for carrying out chemical reactions. A plate heat exchanger has, in a well-known manner, a plurality of plates, with a gap channel being formed between each two adjacent plates. The gap channels are generally divided into two groups, and the gap channels of one group usually alternate with the gap channels of the other group. The two groups of gap channels are fluidically separated from one another but thermally coupled. In conventional operation of a plate heat exchanger, for example, a heat transfer medium flows through the gap channels of both the one and the other group, and an efficient exchange of thermal energy takes place between the heat transfer media.

[0017] According to the invention, selected splitting channels, in particular at least one group of splitting channels, are used to carry out or operate an exothermic reaction therein. These splitting channels provided or used for the exothermic reaction are referred to herein as primary splitting channels. According to the invention, a catalyst material is provided in the primary splitting channels, in particular one for an oxidation reaction of hydrogen, preferably a catalytic combustion of hydrogen with oxygen. A primary fluid is supplied to the primary splitting channels for the reaction. This fluid can also be referred to as the reaction fluid.

[0018] The other group of gap channels, referred to here as secondary gap channels, can be used, for example, to remove the heat released during the exothermic reaction. In this configuration, one can also say that the primary gap channels serve as reaction gap channels and the secondary gap channels as cooling gap channels. A secondary fluid is supplied to the secondary gap channels. If this is used for heat removal, one can say that the secondary fluid serves as a cooling medium. It can be a "classic" heat transfer fluid, e.g. water or thermal oil, which is heated using the heat from the exothermic oxidation reaction. For example, water can be heated to saturated steam or superheated steam.

[0019] It is also possible that the heat from the exothermic oxidation reaction on the primary side is used to drive an endothermic reaction on the secondary side or that cooling is achieved via an endothermic reaction on the secondary side.

[0020] Optionally, a catalyst material can also be provided in the secondary splitting channels. Any catalyst material present in the secondary splitting channels, which can also be referred to as "secondary catalyst material" for differentiation, can differ from the catalyst material in the primary splitting channels.

[0021] Within the scope of the present invention, various exothermic and endothermic reactions can be combined. Alternatively or additionally, secondary gap channels can be used as heating / cooling channels, through which a heat transfer fluid can flow.

[0022] The reactor according to the invention is in particular a thermocatalytic reactor.

[0023] The reactor according to the invention is not an electrolytic reactor. In other words, it is not a reactor in which electrically driven chemical reactions, in particular redox reactions forced by electrical energy, can or do take place. Accordingly, within the scope of the process according to the invention, no electrolytic reactions are carried out in the primary or secondary gap channels.

[0024] For practical purposes, the primary gap channels and the secondary gap channels are not fluidically connected to each other.

[0025] It has also proven particularly advantageous in the reactor according to the invention if the primary and secondary splitting channels are arranged alternately, in other words, if a primary splitting channel alternates with a secondary splitting channel. This allows, for example, particularly efficient cooling of an exothermic reaction on the primary side to be achieved.

[0026] According to the invention, it is further provided that the plate heat exchanger is installed in a pressure shell in which an increased pressure exists or can be achieved during operation. The plate heat exchanger is arranged in the interior of the pressure vessel, so that during operation there is no or only a slight pressure difference to the outside, in other words compared to the pressurized interior of the pressure vessel. The plate heat exchanger can therefore be designed comparatively simply in terms of construction. High pressures and temperatures can prevail in the secondary gap channels and / or the primary gap channels during operation without the need for complex sealing of the plate heat exchanger or the secondary and / or primary gap channels.In particular, it may be the case that the pressure in the pressure vessel and on the high-pressure side of the plate heat exchanger, which may in particular be the secondary side, is at least approximately the same during operation. It should be noted that it is also not excluded that a reactor according to the invention may have more than one plate heat exchanger arranged in the pressure vessel.

[0027] The present invention combines various advantages. Firstly, the reactor according to the invention can be manufactured comparatively cost-effectively. At the same time, it offers a high degree of safety. It provides good heat integration, particularly compared to adiabatic beds with intermediate cooling. It offers high load flexibility, and rapid load changes can also occur. This is particularly true because cooling can be used instead of adiabatic beds. Furthermore, the reactor according to the invention can also be started up comparatively quickly. For example, the secondary fluid can also be used for preheating or heating during a start-up phase, which will be discussed in more detail below.

[0028] In a preferred embodiment, the pressure vessel has an at least substantially cylindrical, in particular circular-cylindrical, shape. It can have a (circular) hollow cylindrical shell that is closed at both ends. It can have rounded, in particular convexly curved ends or end walls, which has proven to be a particularly advantageous shape for pressure vessels. A cylindrical pressure vessel with rounded, outwardly curved end faces can represent a good compromise between the ideal shape of a spherical shell on the one hand and comparatively simple, cost-effective production while still maintaining very good pressure resistance.

[0029] The pressure vessel is preferably designed to be explosion-proof so that a particularly high level of safety can be achieved.

[0030] The pressure vessel can be provided on the inside with an insulating layer made of a thermally insulating material. Purely examples of thermally insulating materials include firebricks, glass fabric and / or ceramic fabric, e.g., polycrystalline mullite / aluminum oxide wool (PCW). Alternatively or additionally, the pressure vessel can comprise steel, in particular an outer shell made of steel. If the pressure vessel comprises an internal thermal insulation layer, its outer shell can be prevented from heating to high temperatures during operation. This makes it possible to provide an outer shell made of less temperature-resistant materials, in particular one made of inexpensive steels that can, for example, only withstand temperatures of a maximum of 250°C, preferably a maximum of 220°C, particularly preferably a maximum of 100°C.

[0031] A leakage sensor can also be provided to monitor the plate heat exchanger. The plate heat exchanger can be monitored for leaks using a leakage sensor. The leakage sensor for monitoring the plate heat exchanger is preferably arranged inside the pressure vessel. If the pressure vessel is or will be filled with inert gas, it is expediently monitored for a component from the plate heat exchanger that is dissimilar to the inert gas. If the pressure vessel is filled with dry air or nitrogen, for example, and high-pressure steam is generated in the secondary side of the plate heat exchanger, the humidity in the pressure vessel can be monitored. For example, if endothermic methanol steam reforming is taking place and N2 is supplied to the pressure vessel as pressurized gas, in other words if it is purged with N2, the leakage sensor is expediently used to test or monitor for H2, CO2, or H2O.

[0032] In principle, various catalyst materials can be used within the scope of the present invention.

[0033] The catalyst material provided in the primary gap channel(s) may, for example, comprise at least one noble metal, in particular platinum and / or palladium, preferably platinum provided on a metal oxide support, in particular platinum provided on an aluminum oxide support.

[0034] As noted, in a further development, a catalyst material for an endothermic reaction, in particular a catalyst material for a hydrogen release reaction, in particular for NH3 cracking or methanol dehydrogenation or methanol reforming or DME reforming or methane steam reforming or LPG reforming or butane or propane dehydrogenation, can be provided in at least one of the secondary cracking channels, preferably in all secondary cracking channels. If a catalyst material is also provided in the secondary cracking channels, this can comprise, for example, copper and / or palladium and / or zinc.

[0035] The catalyst material provided in the primary splitting channel(s) and any catalyst material provided in the secondary splitting channels can also be located on a support material. The (respective) catalyst material or the support material of such a material can, for example, be granular. It can be in the form of pellets, or pellets comprising the catalyst material can be provided in the primary splitting channels. Alternatively or additionally, the catalyst material can also be in the form of at least one coating, obtained, for example, by washcoating. For example, plates of the plate heat exchanger can be coated with the catalyst material or a coating material comprising the catalyst material. One or more insert plates can also be arranged in the primary splitting channels and / or in the secondary splitting channels.which consist of the catalyst material or are coated with the catalyst material, for example, by washcoat, which can simplify production. It is also possible for the catalyst material to be present in the form of catalytically active structures. For example, catalytically active meshes can be provided in the primary and / or secondary splitting channels.

[0036] In a particularly preferred embodiment, a catalytic oxidation reaction is carried out in the primary splitting channel(s). An oxidation reaction of hydrogen, preferably a catalytic combustion of hydrogen with oxygen, can be carried out. In a preferred embodiment, the primary splitting channel(s) accordingly comprise a catalyst material for such a reaction.

[0037] The following may apply: H2(g) + ½ O2(g) -> H2O(g) ΔH° = -242 kJ mol -1

[0038] A combustion mixture comprising a gaseous fuel and a gaseous oxidizing agent can be supplied to the at least one primary gap channel as the primary fluid.

[0039] In a particularly advantageous embodiment, catalytic oxidation of hydrogen takes place under the conditions described in DE 10 2023 200 245 B3.

[0040] In particular, a primary fluid comprising or consisting of a mixture of hydrogen and oxygen is supplied to the at least one primary gap channel, preferably a primary fluid being supplied which is located outside the explosive region.

[0041] The oxygen concentration of the primary fluid is preferably below the oxygen limit concentration.

[0042] The explosive range or explosion range is the range of mixing ratios of components of the primary fluid in which the primary fluid is explosive. The primary fluid is expediently located outside the explosive range; in particular, the oxygen concentration of the primary fluid is below the limiting oxygen concentration. The limiting oxygen concentration indicates the oxygen content below which an overall mixture is no longer explosive. There is not enough oxygen present to enable an explosion. Thus, a flame independent of the ignition source can no longer propagate independently. In particular, an explosive primary fluid is not present at any point in the process according to the invention. How this is achieved in terms of process technology can be found in DE 10 2023 200 245 B3. In this way, the technical effort can be significantly reduced.At the same time, safety can be ensured in a simple and effective manner. Furthermore, the combustion process is particularly efficient. Furthermore, no NOx emissions are produced.

[0043] In an advantageous embodiment, water can be heated to saturated steam or superheated steam by means of the exothermic reaction taking place in the primary cracking channels, in particular the catalytic oxidation reaction of hydrogen. In this case, liquid water is supplied to the secondary cracking channel(s) as a secondary fluid and evaporated while absorbing heat from the exothermic reaction taking place in the primary cracking channels - for example the catalytic oxidation reaction of hydrogen. For example, a pressure of 165 bar can be present in the secondary cracking channels, and liquid water at 340°C can be supplied to the secondary cracking channels as a secondary fluid. The pressure vessel then preferably has at least a similar pressure, in particular also a pressure of 165 bar. The primary cracking channels can also have a similar pressure, or a different pressure, for example atmospheric pressure.

[0044] It is also possible for a retentate stream, particularly originating from product processing, to be used as the primary fluid or to be a component of the primary fluid. In an advantageous development, it can be provided that a primary fluid comprising a retentate, particularly originating from product processing, or a retentate stream is supplied to the at least one primary gap channel.

[0045] A further preferred embodiment is characterized in that a methanol reforming reaction is carried out in the at least one secondary cracking channel, and a catalytic oxidation reaction of a portion of the product stream exiting the at least one secondary cracking channel is carried out in the at least one primary cracking channel. This combination of endothermic reaction on the secondary side and exothermic reaction on the primary side has proven particularly suitable within the scope of the present invention.

[0046] In particular, the following may apply: CH3OH + H2O -> CO2 + 3 H2 ΔH° = +49.7 kJ mol-1

[0047] In the secondary cracking channels, in which the methanol reforming takes place, there is then a methanol reforming catalyst, which comprises or consists of, for example, Cu or Pd / Zn.

[0048] Catalytic oxidation takes place in the primary cracking channels for heating purposes. A portion of the product stream, which consists predominantly of hydrogen (and CO2) and contains smaller amounts of methanol, H2O, and CO, is preferably used for this purpose. The hydrogen, as a valuable product, can be further utilized, for example, in chemical reactions for steel production or electricity generation. Typically, a separation process takes place, such as membrane separation or pressure swing adsorption, which produces a retentate (poor in hydrogen, rich in CO2) and a permeate (rich in hydrogen). The hydrogen-rich permeate serves as the valuable product. The retentate still contains oxidizable substances (hydrogen, CO, methanol), which can be used for heating. Preferably, the retentate or a portion of the retentate is used for heating.In other words, it can be provided that the retentate of a separation process of the product stream, for example from a membrane separation or pressure swing adsorption, is fed to the at least one primary splitting channel as a primary fluid or as a component of the primary fluid.

[0049] It is then further preferred that oxidizable species, in particular hydrogen and / or methanol and / or CO, are oxidized to CO2 with an oxidizing agent, for example atmospheric oxygen, and thereby the required heat for the endothermic reaction on the secondary side is provided.

[0050] For the combination of methanol reforming (endothermic, secondary side) and catalytic oxidation reaction (exothermic, primary side), it is preferred that a pressure of up to 25 bar prevails in the pressure vessel (similar to the methanol reforming pressure in the secondary cracking channels).

[0051] The reactor according to the invention can comprise pressure control means which are designed and / or arranged in such a way that by means of these, the pressure difference which prevails during operation of the reactor between the pressure in the pressure vessel and the pressure in at least one of the secondary gap channels, preferably in all secondary gap channels, can be adjusted, preferably regulated.

[0052] In an advantageous development of the method according to the invention, it is provided that the reactor is operated in such a way that the pressure in the pressure vessel is a maximum of 20%, in particular a maximum of 10%, preferably a maximum of 5%, particularly preferably a maximum of 1% above or below the pressure in at least one of the secondary gap channels, preferably in all of the secondary gap channels, which has proven to be particularly suitable. Alternatively or additionally, the reactor can be operated in such a way that the pressure in the pressure vessel is a maximum of 5 bar, in particular a maximum of 1 bar, preferably a maximum of 100 mbar above or below the pressure in at least one of the secondary gap channels, preferably in all of the secondary gap channels. In other words, when setting orControl of a maximum pressure difference between the interior of the pressure vessel and the pressure in one or more secondary gap channels can be based on a percentage difference and / or absolute deviations.

[0053] Pressure control means of the reactor according to the invention can be designed and / or arranged to realize this.

[0054] In other words, the pressure in the pressure vessel is then the same or at least similar to that in one or more secondary gap channels. For this purpose, the pressure of the compressed gas can be adjusted during operation, for example, to the pressure in the secondary gap channel(s). The pressure control means can be designed and / or configured accordingly.

[0055] If pressure control means are present, these can alternatively or additionally be designed and / or arranged in such a way that by means of them the pressure difference which prevails during operation of the reactor between the pressure in at least one of the primary gap channels, preferably in all primary gap channels, and the pressure in at least one of the secondary gap channels, preferably in all secondary gap channels, can be adjusted, preferably regulated.

[0056] The reactor can further be operated such that the pressure in at least one of the secondary gap channels, preferably the pressure in all secondary gap channels, is a maximum of 20%, in particular a maximum of 10%, preferably a maximum of 5%, particularly preferably a maximum of 1% above or below the pressure in at least one of the primary gap channels, preferably in all primary gap channels. Alternatively or additionally, the reactor can be operated such that the pressure in at least one of the secondary gap channels, preferably the pressure in all secondary gap channels, is a maximum of 5 bar, in particular a maximum of 1 bar, preferably a maximum of 100 mbar above or below the pressure in at least one of the primary gap channels, preferably in all primary gap channels.

[0057] Pressure control means of the reactor according to the invention can be designed and / or arranged to realize this.

[0058] In other words, the operation can also be carried out in such a way that the secondary gap channels have the same or similar pressure as the primary gap channels.

[0059] However, a pressure difference may also be present, although (significantly) different pressures are also possible in principle. The secondary gap channels and / or the primary gap channels, or the plates defining the secondary gap channels and / or the plates defining the primary gap channels, can then be welded together, or suitable seals and sufficient contact pressure between the plates can be implemented to enable even higher pressure differences.

[0060] It can also be provided that the primary gap channels and / or the secondary gap channels are provided with stabilizing elements, in particular stabilizing webs. The stabilizing elements can increase stability. Particularly for applications in which larger pressure differences between the primary and secondary gap channels occur, it can be advantageous to reinforce the gap channels accordingly. Stabilizing elements, for example in the form of stabilizing webs, can extend between two adjacent plates and be supported on the adjacent plates.

[0061] In the event that a larger pressure difference between the primary and secondary gap channels occurs or is to be possible during operation, for example a pressure difference of more than 5 bar, possibly even significantly more than 5 bar, the seal of the plate heat exchanger can be specifically designed such that the side with the higher pressure (primary or secondary side) keeps the side with the lower pressure (secondary or primary side) sealed during operation. In particular, sealing elements of the plate heat exchanger can be specifically arranged accordingly. For example, in such a way that, due to the higher pressure on one side (primary or secondary), at least one element, such as a plate of the plate heat exchanger, presses them against at least one other element of the plate heat exchanger during operation.

[0062] In a further advantageous embodiment, a control device is provided by means of which the pressure in the pressure vessel and / or the pressure difference between the pressure in the pressure vessel and the pressure in at least one of the secondary gap channels can be adjusted, preferably regulated. Alternatively or additionally, the pressure in the primary gap channels can be adjusted, preferably regulated, using the control device.

[0063] A pressure measuring device for measuring the pressure in the pressure vessel and at least one secondary pressure measuring device for measuring the pressure in one or more, possibly all, secondary gap channels can also be provided. Alternatively or additionally, the reactor according to the invention can comprise a secondary differential pressure measuring device for measuring the pressure difference between the pressure in the pressure vessel and the pressure in at least one of the secondary gap channels.

[0064] At least one primary pressure measuring device can also be provided for measuring the pressure in one or more, possibly all, primary gap channels. Alternatively or additionally, the reactor according to the invention can comprise a primary differential pressure measuring device for measuring the pressure difference between the pressure in the pressure vessel and the pressure in at least one of the primary gap channels.

[0065] The pressure measuring device and / or the secondary pressure measuring device and / or the primary pressure measuring device and / or the secondary differential pressure measuring device and / or the primary differential pressure measuring device may be part of the pressure control means of the reactor.

[0066] A control device of the pressure control means can also be connected to the pressure measuring device and / or the secondary pressure measuring device and / or the primary pressure measuring device and / or the secondary differential pressure measuring device and / or the primary differential pressure measuring device. Depending on the detected pressure (difference) measured values, for example, at least one valve and / or at least one pump and / or at least one compressor can be controlled in order to achieve the desired pressure situation. The pressure fluid supply means, which can comprise at least one valve and / or at least one pump and / or at least one compressor, can also be connected to the pressure control means, in particular to a control device thereof.

[0067] It has also proven particularly advantageous if the pressure control means, in particular a control device thereof, are designed and / or configured in such a way that by means of said means the pressure in the pressure vessel can be adjusted, in particular regulated, as a function of the pressure in at least one of the secondary gap channels and / or as a function of the pressure difference between the pressure in the pressure vessel and the pressure in at least one of the secondary gap channels.

[0068] Alternatively or additionally, the pressure control means, in particular a control device thereof, can be designed and / or configured such that by means of said means the pressure in at least one of the primary gap channels can be adjusted, in particular regulated, as a function of the pressure in at least one of the secondary gap channels and / or as a function of the pressure difference between the pressure in the pressure vessel and the pressure in at least one of the primary gap channels.

[0069] For example, the control device of the pressure control means may conveniently be connected to the primary fluid and / or the secondary fluid supply means.

[0070] The control device can further be designed and / or configured to achieve maximum pressure deviations in the aforementioned ranges. The primary fluid supply means and / or the secondary fluid supply means and / or the pressurized fluid supply means can each comprise at least one line or be provided by at least one line. The primary fluid supply means can also comprise at least one compressor and / or at least one pump and / or at least one valve, which has proven particularly expedient. Analogously, the secondary fluid supply means can comprise at least one compressor and / or at least one pump and / or at least one valve. The pressurized fluid supply means can also have at least one compressor and / or at least one pump and / or at least one valve.It should be emphasized that, although the aforementioned supply means may each comprise at least one compressor and / or at least one pump and / or at least one valve, this need not be the case. In the simplest case, these may each consist of only one supply line or one inlet.

[0071] The pressure fluid supplied to the pressure vessel can, for example, be N 2 and / or liquid water and / or water vapor and / or air or be provided by it.

[0072] It should be noted that, in a preferred embodiment, primary fluid is preheated before it enters the primary fluid channel(s), for example by means of a heat exchanger provided for primary fluid preheating.

[0073] In an advantageous development, the pressure fluid can also be tempered, in particular heated or cooled. The reactor according to the invention can accordingly comprise a pressure fluid tempering device for tempering the pressure fluid. It can be provided that the pressure fluid is or can be cooled and / or heated before entering the pressure vessel and / or after exiting the pressure vessel. The pressure fluid tempering device, if present, can be designed and arranged accordingly.

[0074] A further advantageous embodiment is further characterized in that the pressure fluid is at least partially exchanged repeatedly or continuously. Alternatively or additionally, it can be provided that pressure fluid removed from the pressure vessel is returned to the pressure vessel, preferably following cooling and / or heating.

[0075] The reactor according to the invention can comprise a pressure fluid circuit via which pressure fluid can be discharged from the pressure vessel and fed back into the pressure vessel.

[0076] It can be provided that at least one, preferably all, secondary gap channels are supplied with, in particular, boiling methanol or, in particular, boiling water or thermal oil or a molten salt or gas, e.g., compressed air, as a secondary fluid. The plate heat exchanger of the reactor according to the invention, in particular its secondary gap channels, can be designed accordingly in a further development, for example, made of a suitable material.

[0077] A suitable heat transfer medium as a secondary fluid, which can be heated via the exothermic reaction on the primary side, can be selected depending on the temperature. Boiling methanol, for example, has proven particularly suitable for a temperature range of 70°C to 130°C. Boiling water for a temperature range of 130°C to 350°C, which roughly corresponds to a boiling pressure of 2.7 to 165 bar. A thermal oil is particularly suitable for a comparatively high temperature range of 250°C to 450°C, preferably 300°C to 450°C. The same applies to molten salt, which has proven particularly suitable for a temperature range greater than or equal to 400°C, for example in the range of 400°C to 650°C.

[0078] It is also possible to carry out an endothermic reaction on the secondary side of the plate heat exchanger, which has proven particularly advantageous. Accordingly, in an advantageous development, the reactor according to the invention can be characterized in that a catalyst material for an endothermic reaction, in particular a catalyst material for a hydrogen release reaction, preferably for ammonia cracking or DME reforming or methane steam reforming or LPG reforming or butane or propane dehydrogenation, is provided in at least one of the secondary cracking channels, preferably in all secondary cracking channels.

[0079] In the process according to the invention, it can be provided that a reaction fluid for an endothermic reaction is also supplied to the at least one secondary cracking channel as a secondary fluid, and that an endothermic reaction, in particular a hydrogen release reaction, preferably an ammonia cracking reaction or a DME reforming reaction or a methane steam reforming reaction or an LPG reforming reaction or a butane or propane dehydrogenation reaction, is carried out in the at least one secondary cracking channel. For example, a hydrogen-rich compound can be supplied to the at least one secondary cracking channel, preferably to all secondary cracking channels, as a secondary fluid.

[0080] In a start-up phase for starting the endothermic process, or when electricity costs are low, the plate heat exchanger can be heated, preferably electrically, to provide heat for the endothermic reaction and to start or continue it, in particular a hydrogen release reaction.

[0081] In an advantageous development, the plate heat exchanger according to the invention can comprise a preferably electrical heating device. For example, one or more plates of the plate heat exchanger can be heated, preferably electrically, by means of the heating device. If a heating device is present, it can be used to provide heat for an endothermic reaction in the secondary gap channels during a start-up phase or when electricity costs are low.

[0082] It is also possible to supply a heated fluid or gas to at least one primary splitting channel, preferably all primary splitting channels, during a start-up phase in order to preheat the catalyst and start the endothermic reaction. This form of heating can be used alternatively or in addition to electrical heating of the plate heat exchanger, for example, its plates.

[0083] Alternatively or additionally, the secondary side can be used to heat the reactor for startup. For example, if a thermal oil is supplied as the secondary fluid, the thermal oil or the thermal oil circuit can be heated. The reactor according to the invention can be designed to include heating means for heating the secondary fluid. In this case, for example, electric heating plates in the reactor can be dispensed with.

[0084] A further advantageous embodiment of the invention is characterized in that the secondary fluid is evaporated and / or superheated as a result of the absorption of heat released during the exothermic reaction in the at least one primary gap channel. It is also possible for heated secondary fluid to be used to generate steam, in particular superheated steam. The generated and / or superheated steam can then, for example, be fed to at least one solid oxide electrolyzer cell to produce hydrogen, preferably, the hydrogen produced is subsequently used to produce ammonia (NH 3 ). Such a configuration has proven to be particularly energy-efficient. The reactor according to the invention can accordingly comprise at least one solid oxide electrolyzer cell.

[0085] Furthermore, it can be provided that at least one of the secondary gap channels is subdivided into several partial secondary gap channels, preferably connected in parallel flow terms. Such subdivision or division, so to speak into several "sub-secondary gap channels," can also be provided for all secondary gap channels.

[0086] Alternatively or additionally, at least one of the secondary fission channels, or even all of the secondary fission channels, may have a meandering course. If there is a subdivision or division into several "sub-secondary fission channels," these may also be meandering.

[0087] It has also proven to be advantageous if the primary gap channels are connected to one another via a primary distribution channel and a primary collector channel.

[0088] Alternatively or additionally, it can be provided in an analogous manner that the secondary gap channels are connected to one another via a secondary distribution channel and a secondary collector channel.

[0089] For example, four, in particular round, holes can be provided in each plate, wherein the holes are located at identical locations in all plates and the holes of all plates are aligned, and each aligned hole forms a primary / secondary distributor or collector channel, in particular a cylindrical one, extending transversely through the plates and the gap channels defined between them. If four holes are provided in each plate, in particular a primary distributor channel and a primary collector channel, as well as a secondary distributor channel and a secondary collector channel, are formed or defined.

[0090] The holes are preferably located near the edges of the panels. If the panels are quadrangular, in particular at least substantially rectangular or square, one of the holes can be located in or near each corner of each panel.

[0091] A further advantageous embodiment of the invention is characterized in that the primary gap channels of the plate heat exchanger are connected to a particularly central primary inlet line and a particularly central primary outlet line. Similarly, the secondary gap channels can be connected to a particularly central secondary inlet line and a particularly central secondary outlet line.

[0092] The primary gap channels can, for example, be connected to a primary inlet line via a primary distribution channel and to a primary outlet line via a primary collector channel. The secondary gap channels can be connected in a similar manner to a secondary inlet line via a secondary distribution channel and to a secondary outlet line via a secondary collector channel.

[0093] As a rule, the plates of the plate heat exchanger will have the same shape, for example, they will all be at least approximately rectangular, and / or have the same external dimensions. It is also possible for several, or even all, plates of the plate heat exchanger to be identical in construction. The plates are preferably made of metal or comprise such a material.

[0094] Alternatively or additionally, the plates have a structured surface or profile on at least one side. Advantageously, the at least one side having a structured surface or profile is a side defining or delimiting a gap channel.

[0095] In an advantageous development, the plate heat exchanger can be provided with an insulating layer made of a thermally insulating material on its exterior. This prevents excessive heating of the pressure vessel surrounding the plate heat exchanger during operation.

[0096] The plate heat exchanger may further comprise a housing. In this case, the housing may, in particular, have an insulating layer made of a thermally insulating material.

[0097] The invention also relates to the use of a reactor according to the invention for a catalytic oxidation reaction, in particular for a catalytic oxidation reaction of hydrogen, preferably a catalytic combustion of hydrogen with oxygen, and / or for a hydrogen release reaction, in particular for an NH3 cracking or a methanol reforming or a DME reforming or a methane steam reforming or an LPG reforming or a butane or propane dehydrogenation, and / or for heating water to saturated steam or superheated steam.

[0098] The combination of a catalytic oxidation reaction (exothermic), in particular a catalytic oxidation reaction of hydrogen, preferably a catalytic combustion of hydrogen with oxygen, on the primary side and the heating of water to saturated steam or superheated steam on the secondary side (using the heat released on the primary side) has proven particularly suitable. Another particularly advantageous combination consists of a catalytic oxidation reaction (exothermic), in particular a catalytic oxidation reaction of hydrogen, preferably a catalytic combustion of hydrogen with oxygen, on the primary side and methanol reforming (endothermic) on the secondary side.

[0099] With regard to the embodiments of the invention, reference is also made to the dependent claims and to the following description with reference to the accompanying drawings. In the drawing: Fig. 1 an embodiment of a reactor according to the invention in a purely schematic sectional view, Fig. 2 a perspective external view of the reactor Fig. 1, and Fig. 3 another purely schematic sectional view of the reactor from Fig. 1.

[0100] The same reference numerals are used in the figures for identical or similar components and elements.

[0101] The Fig. 1 shows a purely schematic sectional view of a first embodiment of a reactor 1 according to the invention. Fig. 2 shows the reactor 1 in a perspective external view and the Fig. 3 another schematic sectional view.

[0102] Reactor 1 is designed to carry out exothermic reactions.

[0103] The reactor 1 comprises a plate heat exchanger 2 with a plurality of adjacent, in particular at least substantially parallel oriented, plates 3. Of the plates 3, Fig. 1, only a few are provided with the reference numeral 3 as an example. The plates 3, which are made of metal, all have a rectangular outer contour and the same dimensions in the embodiment shown here; in other words, they are all the same size.

[0104] Gap channels 4, 5 are defined between the plates 3, specifically one gap channel 4, 5 between each two adjacent plates 3. The gap channels 4, 5 are divided into two groups, namely several primary gap channels 4 which are fluidically connected to one another and specifically connected in parallel, and several secondary gap channels 5 which are fluidically connected to one another and specifically connected in parallel. The gap channels 4 of one group, the primary gap channels 4, alternate with the gap channels 5 of the other group, the secondary gap channels 5. A primary fissure canal 4 is therefore located between two secondary fissure canals 5 or - in the case of the primary fissure canal 4 on the far left in the figure at the edge - next to a secondary fissure canal 5. In an analogous manner, a secondary fissure canal 5 is located between two primary fissure canals 4 or - in the case of the secondary fissure canal 5 on the far right in the figure at the edge - next to a primary fissure canal 4.

[0105] In each of the primary gap channels 4 there is a catalyst material 6 for an exothermic reaction. In the highly simplified, purely schematic Fig. 1, the catalyst material 6 is only indicated as an example in some primary gap channels 4. In the Fig. 1 schematically shows a granular catalyst material 6 as an example, even if only over a section of the respective primary splitting channel 4. It is understood that the primary splitting channels 4 can be filled over their entire length with, for example, granular catalyst material 6. Alternatively or additionally, it is also possible for the plates 3 to be coated with catalyst material 6 or a coating material comprising catalyst material 6. One or more insert plates can also be arranged in the primary splitting channels 4, which insert plates consist of the catalyst material or are coated with the catalyst material, for example by washcoat, which can simplify production. It is also possible for the catalyst material to be in the form of catalytically active structures. By way of example, catalytically active networks can be provided in the primary splitting channels and / or the secondary splitting channels.

[0106] It should be noted that the internal structure of the plate heat exchanger 2, including the plates 3, primary and secondary gap channels 4, 5 and the catalyst material 6, is only shown in Fig. 1 recognizable, in Fig. 2 is not shown again.

[0107] This catalyst material 6 is for a catalytic oxidation reaction of hydrogen, in particular a catalytic combustion of hydrogen with oxygen. The following applies to the oxidation reaction: H2(g) + 1 / 2 O2(g) -> H2O(g) ΔH° = -242 kJ mol -1

[0108] In the illustrated embodiment, a catalyst material 6 comprising or consisting of platinum, specifically platinum provided on a metal oxide support, is provided in the primary gap channels 4. The same catalyst material 6 is present in all primary gap channels 4.

[0109] The reactor 1 further comprises primary fluid supply means 7 for supplying a primary fluid to the primary gap channels 4. In the illustrated example, a combustion mixture comprising a gaseous fuel and a gaseous oxidant is supplied as the primary fluid. Specifically, a primary fluid comprising a mixture of hydrogen and oxygen is supplied. The primary fluid is located outside the explosive range. The oxygen concentration of the primary fluid is below the oxygen limit concentration.

[0110] The primary fluid can also be referred to as reaction fluid or reaction gas. The primary fluid supply means 7 comprise at least one blower / compressor and / or at least one valve, which in the purely schematic Fig. 1 are not shown separately.

[0111] How to Fig. 1, the primary gap channels 4 are all fluidically connected on the inlet side to a central primary distribution channel 8, which in the illustrated embodiment is a component of the primary fluid supply means 7. During operation, the primary fluid enters the primary distribution channel 8 via the Fig. 1 central primary inlet line 9 of the primary fluid supply means 7 indicated by an arrow. Supplied primary fluid can be distributed to all primary gap channels 4 via the primary distribution channel 8.

[0112] The reactor 1 also comprises secondary fluid supply means 10 for supplying a secondary fluid to the secondary gap channels 5. The secondary fluid supply means 10 comprise at least one pump and / or at least one valve, which in the purely schematic Fig. 1 are not shown separately.

[0113] The secondary gap channels 5 are—analogous to the primary gap channels 4—all fluidically connected on the inlet side to a central secondary distribution channel 11, which in the illustrated embodiment is a component of the secondary fluid supply means 10. During operation, the secondary fluid enters the secondary distribution channel 11 via the upstream, central secondary inlet line 12 of the secondary fluid supply means 10.

[0114] On the outlet side of the primary gap channels 4, a primary collector channel 13 is provided, in which fluid emerging from all primary gap channels 4 is collected and can exit the plate heat exchanger 2 via a central primary outlet line 14.

[0115] On the outlet side of the secondary gap channels 5, a secondary collector channel 15 is provided in an analogous manner, in which fluid emerging from all secondary gap channels 5 is collected and can exit from the plate heat exchanger 2 via a central secondary outlet line 16.

[0116] The primary gap channels 4 and the secondary gap channels 5 are not fluidically connected to each other.

[0117] In the embodiment shown here, the plate heat exchanger 2 has a cuboid-shaped housing 17, through the wall of which the inlet and outlet lines 9, 12, 14, 16 for the primary and secondary fluid extend.

[0118] It should be noted that in the schematic Fig. 1, the two distributor and collector channels 8, 11, 13, 15 are shown above and below the plates 3 for reasons of clarity. However, these can also extend through the plates 3, in particular be defined by recesses provided in the plates 3. For example, four, in particular round, holes (not shown in the figure) can be provided in each plate 3, wherein the holes are located at identical locations in all plates 3 and the holes in all plates 3 are aligned, wherein each aligned hole forms a, in particular cylindrical, primary or secondary distributor or collector channel 8, 11, 13, 15 extending transversely through the plates 3 and the gap channels 4, 5 defined between them. This is already known from conventional or conventionally used plate heat exchangers. The connection of the respective distributor or collector channel 8, 11, 13, 15 with the associated gap channels orThe separation can then be achieved via seals (not shown), as is well known from conventional plate heat exchangers. The holes are preferably located in the edge region of the plates 3. If the plates 3 are square, as in the illustrated embodiment, one of the holes can be located in or near each corner.

[0119] In the embodiment shown here with an exothermic reaction on the primary side, a cooling fluid, e.g. boiling methanol, boiling water, a thermal oil or even a molten salt, is used as the secondary fluid.

[0120] The reactor 1 also comprises a pressure vessel 18 surrounding the plate heat exchanger 2. As can be seen in the figures, the pressure vessel 18 has a hollow cylindrical shell section and rounded, outwardly curved end faces. The cube- or cuboid-shaped plate heat exchanger 2 is arranged in the pressure vessel 18.

[0121] The pressure vessel 18 comprises an outer shell made of inexpensive steel, which is provided on the inside with an insulating layer made of a thermally insulating material. The thermal insulation ensures or contributes to the outer shell having a temperature of no more than 200°C, preferably no more than 70°C, during operation, which enables the use of inexpensive steels. It should be noted that alternatively or additionally, the plate heat exchanger 2, e.g. its housing 17, can be provided with an insulating layer made of a thermally insulating material. The pressure vessel 18 is formed in two parts, with a first part 18a and a second part 18b. The two parts 18a, 18b are detachably connected to one another via molded flanges 18c and screws (not visible in the figures).The plate heat exchanger 2 is held in the pressure vessel 18 by means of a holder 18d, which is preferably fastened to the flanges 18c, at a distance from the pressure vessel wall (cf. Fig. 3). In addition, depending on the length of the plate heat exchanger 2, further supports can be provided, particularly in the pressure vessel part 18a. It should be noted that in the purely schematic, simplified Fig. 1 the two-part design of the pressure vessel 18 is not recognizable.

[0122] Furthermore, pressure fluid supply means 19 are provided, which are designed to supply a pressure fluid to the interior 20 of the pressure vessel 18 and to generate an increased pressure of at least 2 bar, in particular of at least 5 bar, preferably of at least 10 bar, particularly preferably of at least 20 bar in the interior 20 of the pressure vessel 18. The pressure fluid supply means 19 comprise at least one compressor and / or at least one valve, which are shown in the schematic Fig. 1 are not shown separately.

[0123] The pressure vessel 18 and the pressure fluid supply means 19 enable the plate heat exchanger 2 to have no or only a small pressure difference during operation, when the exothermic reaction is carried out on the primary side and, if appropriate, an endothermic reaction is carried out on the secondary side, in particular between the secondary gap channels 5 and the interior 20 of the pressure vessel 18, and the plate heat exchanger 2 can therefore be designed more simply with regard to its seals.

[0124] It should be noted that in the schematic, highly simplified Fig. 1 the seals, which in particular prevent the escape of primary and secondary fluid into the pressure vessel 18 or the entry of pressure fluid into the primary and secondary gap channels 4, 5, are not shown.

[0125] By means of the pressure fluid supply means 19, a pressure fluid can be supplied to the pressure vessel 18, for example, which comprises or is provided by nitrogen or water or water vapor or air.

[0126] Temperature control of the pressure fluid can be provided. Fig. The reactor 1 shown in Figure 1 comprises a pressurized fluid circuit 21 with a pressurized fluid temperature control device, which comprises or is provided by a heat exchanger 22. Compressed gas can be withdrawn from the pressure vessel 18 via the pressurized fluid circuit 21, cooled / heated by means of the pressurized fluid temperature control device, in particular by means of the heat exchanger 22, and reintroduced into the pressure vessel 18. The circuit 21 also comprises a compressor / pump 23. Additional cooling can be achieved via a cycled, cooled pressurized fluid.

[0127] The pressure vessel 18 can also be provided with a leakage sensor (not shown).

[0128] Pressure control means are provided which are designed and / or arranged in such a way that by means of them the pressure difference which prevails during operation of the reactor 1 between the pressure in the pressure vessel 18 and the pressure in the secondary gap channels 5 can be adjusted, preferably regulated.

[0129] The reactor 1, in particular the pressure control means, specifically comprises a control device 24, by means of which the pressure prevailing in the interior 20 of the pressure vessel 18 can be adjusted, preferably regulated. Furthermore, the pressure in the secondary gap channels 5 can be adjusted, preferably regulated, using the control device 24. For this purpose, the control device 24 is expediently connected to the secondary fluid supply means 10 and the pressurized fluid supply means 19, for example, compressors thereof.

[0130] Pressure measuring devices, such as pressure sensors, can be provided for measuring the pressure in the pressure vessel 18 and / or the pressure in at least one secondary gap channel 5. Alternatively or additionally, a secondary differential pressure measuring device can be provided for measuring the pressure difference between the pressure in the pressure vessel 18 and the pressure in at least one of the secondary gap channels 5. Alternatively or additionally, a pressure measuring device can be provided for measuring the pressure in at least one primary gap channel 4. The pressure measuring devices and / or the secondary differential pressure measuring device can be part of the pressure control means. The control device 24 can be connected to the pressure measuring devices and / or the differential pressure measuring device in order to be able to carry out control or regulation depending on the measured pressure values.It is understood that other combinations of pressure measuring devices are also possible and the above is exemplary.

[0131] The pressure vessel 18 has a pressure fluid outlet line 25 in which an outlet valve 26 is arranged. Pressure fluid can escape from the pressure vessel 18 via the pressure fluid outlet line 25. A safety valve can also be provided, which is activated if the pressure is too high (not shown in the figure). Pressure fluid can then be directed via such a safety valve, for example, to a flare or safe location.

[0132] There is also a vent valve 27 for the plate heat exchanger 2.

[0133] During operation of reactor 1, the primary fluid is supplied to the primary gap channels 4, in other words, the primary side of the plate heat exchanger 2, and water, for example, is supplied as a secondary fluid to the secondary gap channels 5, i.e., the secondary side. At the same time, a pressurized fluid, in this case nitrogen or air, is supplied to the pressure vessel.

[0134] It should be noted that the primary fluid or secondary fluid may be preheated before entering the primary gap channels 4 or secondary gap channels 5, respectively. The reactor 1 may include a heat exchanger for primary fluid preheating and / or secondary fluid preheating (not shown).

[0135] In the primary gap channels 4, hydrogen is oxidized according to the above equation, releasing heat. Cooling occurs on the secondary side of the plate heat exchanger 2 via the water flowing through the secondary gap channels 5. Specifically, the water in the secondary gap channels 5 is heated to saturated steam or superheated steam at 165 bar and 350°C via the exothermic, catalytic oxidation reaction of hydrogen on the primary side. The water enters the plate heat exchanger 2, specifically the secondary gap channels 5, in liquid form at 340°C. Saturated steam or superheated steam exits the secondary outlet line 16 at 350°C or more than 350°C.

[0136] The catalytic oxidation of hydrogen takes place in the primary gap channels 4 preferably under the conditions described in DE 10 2023 200 245 B3.

[0137] Additional cooling can be achieved with the Fig. 1 illustrated embodiment via the cooled pressure fluid

[0138] The pressure in the pressure vessel 18 is adjusted to the pressure in the secondary gap channels 5 by means of the control device 24.

[0139] Specifically, the reactor 1 is operated such that the pressure in the pressure vessel 18 is, with the aid of the control device 24, a maximum of 20%, in particular a maximum of 10%, preferably a maximum of 5%, particularly preferably a maximum of 1%, above or below the pressure in the secondary gap channels 5. In the exemplary embodiment described here, the reactor 1 is operated such that the pressure in the pressure vessel 18 is a maximum of 5 bar, in particular a maximum of 1 bar, preferably a maximum of 100 mbar, above or below the pressure in the secondary gap channels 5. The control device 24 is designed and / or configured accordingly.

[0140] The primary side, specifically the primary gap channels 4, can be at the same or similar pressure or at a (significantly) different pressure, for example even at atmospheric pressure. If the same or similar pressure is desired, the reactor 1 can, for example, be operated such that the pressure in the primary gap channels 4 is a maximum of 20%, in particular a maximum of 10%, preferably a maximum of 5%, particularly preferably a maximum of 1%, above or below the pressure in the secondary gap channels 5. Specifically, the reactor 1 can be operated such that the pressure in the primary gap channels 4 is a maximum of 5 bar, in particular a maximum of 1 bar, preferably a maximum of 100 mbar, above or below the pressure in the secondary gap channels 5.

[0141] The control device 24 is designed and / or configured accordingly.

[0142] In particular, if a plate heat exchanger 2 with a more complex seal and stabilizing bars is used, operation with more strongly deviating pressures is also possible.

[0143] The leak sensor of the pressure vessel 18 monitors for a lack of gas. The leak sensor detects a leak between the secondary gap channels 5 and the pressure vessel 18, in particular, when the pressure in the secondary gap channel 5 is slightly higher than in the pressure vessel 18.

[0144] Primary fluid emerging from the primary gap channels 4 on the outlet side after the reaction is collected in the primary collector channel 13 and can be led out of the plate heat exchanger 2 and the pressure vessel 18 via the primary outlet line 14 and fed to a desired use, e.g. heat recovery as described in DE 10 2023 200 245 B3.

[0145] Heated secondary fluid, presently in the form of saturated steam or superheated steam, exits the secondary gap channels 5 on the outlet side. The saturated steam / superheated steam can also be used for a desired purpose.

[0146] It is also possible to carry out an endothermic reaction, e.g. a hydrogen release reaction, on the secondary side of the plate heat exchanger 2 and to use this for the absorption and removal of the heat released in the primary gap channels 4 during the exothermic reaction, in this case the catalytic oxidation reaction of hydrogen.

[0147] If this is the case, a catalyst material for an endothermic reaction, e.g. a hydrogen release reaction, is expediently provided in the secondary gap channels 5 (in Fig.1 not shown). In other words, not only the primary gap channels 4 but also the secondary gap channels 5 can be filled with a catalyst material.

[0148] In this case, a reaction fluid for the endothermic reaction is supplied to the secondary gap channels 5 as the secondary fluid. In other words, a reaction fluid for an endothermic reaction is used as the secondary fluid for cooling. For a hydrogen release reaction, for example, a hydrogen-rich compound would be supplied as the secondary fluid, and hydrogen would be released by absorbing heat from the reaction side.

[0149] An example of a hydrogen release reaction carried out on the secondary side is methanol reforming. In this case, a methanol reforming catalyst material 6 comprising or consisting of Cu or Pd / Zn is expediently arranged in the secondary cracking channels 5.

[0150] It has proven particularly advantageous if methanol reforming is carried out in the secondary splitting channels 5 and a catalytic oxidation reaction of a portion of the product stream is carried out in the primary splitting channels 4. The product stream can consist predominantly of hydrogen (and CO2) and contain smaller amounts of methanol and CO. The primary fluid can be used, in particular, as the retentate of a separation process of the product stream, e.g., from membrane separation or pressure swing adsorption. Together with an oxidizing agent, e.g., atmospheric oxygen, the oxidizable species (hydrogen, methanol, CO) can be oxidized to CO2 on the primary side, thereby providing the heat required for the endothermic methanol reforming on the secondary side.

[0151] In the pressure vessel 18, a pressure is expediently set which amounts to 20 bar (similar to the methanol reforming pressure prevailing in the secondary cracking channels 5 during operation) or deviates from 20 bar by a maximum of the aforementioned pressure or percentage values. This is done in a completely analogous manner to that described above using the example of heating water to saturated steam (secondary side) by means of the catalytic oxidation reaction (primary side). The pressure in the primary cracking channels 4 can also correspond at least approximately to this pressure or deviate more significantly from it, for example, correspond to atmospheric pressure.

[0152] Other endothermic reactions, which have also proven particularly suitable as an alternative to methanol reforming, are - NH3 cracking - DME reforming - Methane steam reforming - LPG reform - Butane / propane dehydrogenation

[0153] In all of these reactions, a retentate stream from product processing can be used to provide heat through oxidation (via the primary side). The catalytic oxidation of hydrogen in the primary cracking channels 4 can in all cases take place under the conditions described in DE 10 2023 200 245 B3.

[0154] If an endothermic reaction is carried out on the secondary side, the plate heat exchanger 2 can be designed to be (electrically) heated in order to provide heat for the endothermic reaction during a start-up phase and / or at low electricity costs. It is also possible for the secondary fluid to be heated, particularly externally.

[0155] If an endothermic reaction, such as an endothermic hydrogen release reaction, is utilized on the secondary side, a hydrogen-rich compound can be supplied as a secondary fluid to the secondary splitting channels 5. Hydrogen release occurs in the secondary splitting channels 5, which in this case are provided with a suitable catalyst material for the endothermic reaction, and hydrogen and a hydrogen-poor compound exit the secondary splitting channels 5 on the outlet side and enter the secondary collector channel 15.

[0156] In the case of a hydrogen release reaction, it has proven particularly efficient if the hydrogen obtained on the secondary side is fed back to the primary side. Reactor 1 can be designed accordingly, in particular, by including suitable lines for such a flow.

[0157] During a start-up phase for starting the process, the plate heat exchanger 2 is then expediently first heated electrically to provide heat for the hydrogen release reaction and to start it. Heated nitrogen can also be supplied to the primary cracking channels 4 during the start-up phase to preheat the catalyst for the endothermic reaction and start the reaction.

[0158] Until hydrogen is available through the hydrogen release reaction, it is expediently stored for the primary side. Another source can be used temporarily for this purpose, e.g., an electrolyzer or a separate hydrogen release reaction device. List of reference symbols 1 reactor 2 plate heat exchangers 3 plates 4 Primary slit canal 5 Secondary slit canal 6 Catalyst material 7 Primary fluid supply means 8 Primary distribution channel 9 Primary inlet line 10 Secondary fluid supply means 11 Secondary distribution channel 12 Secondary inlet line 13 Primary collector channel 14 Primary outlet line 15 Secondary collector channel 16 Secondary outlet line 17 housings 18 pressure vessels Part 18a Part 18b 18c flange 18d bracket 19 Pressure fluid supply means 20 Interior of the pressure vessel 21 Pressure fluid circuit 22 heat exchangers 23 Compressor 24 Control device 25 Pressure outlet line 26 Exhaust valve 27 vent valve

Claims

[1] Reactor (1) for carrying out exothermic reactions comprising - a plate heat exchanger (2) with a plurality of adjacent plates (3), between which gap channels (4, 5) are defined, wherein the gap channels (4, 5) are divided into a plurality of fluidically interconnected, in particular fluidically parallel, primary gap channels (4), and a plurality of fluidically interconnected, in particular fluidically parallel, secondary gap channels (5), wherein in at least one of the primary gap channels (4), preferably in all primary gap channels (4), a catalyst material (6) for an exothermic reaction, in particular for a catalytic oxidation reaction, preferably for a catalytic oxidation reaction of hydrogen, particularly preferably a catalytic combustion of hydrogen with oxygen, is provided,and wherein primary fluid supply means (7) are provided for supplying a primary fluid to the primary gap channels (4) and secondary fluid supply means (10) are provided for supplying a secondary fluid to the secondary gap channels (5), - a pressure vessel (18) surrounding the plate heat exchanger (2), - Pressure fluid supply means (19) which are designed to supply a pressure fluid to the pressure vessel (18) and in particular to generate an increased pressure of at least 2 bar, in particular of at least 5 bar, preferably of at least 10 bar, particularly preferably of at least 20 bar in the pressure vessel (18). [2] Reactor (1) according to claim 1, characterized bythat pressure control means are provided, and the pressure control means are designed and / or arranged such that by means of them the pressure difference which prevails during operation of the reactor (1) between the pressure in the pressure vessel (18) and the pressure in at least one of the secondary gap channels (5), preferably in all secondary gap channels (5), is adjustable, preferably controllable, in particular, wherein the pressure control means are designed and / or arranged to keep the pressure in the pressure vessel (18) during operation of the reactor (1) by a maximum of 20%, in particular by a maximum of 10%, preferably by a maximum of 5%, particularly preferably by a maximum of 1% above or below the pressure in at least one secondary gap channel (5), preferably in all secondary gap channels (5), and / or to keep the pressure in the pressure vessel (18) during operation of the reactor (1) by a maximum of 5 bar, in particular by a maximum of 1 bar,preferably by a maximum of 100 mbar above or below the pressure in at least one of the secondary gap channels (5), preferably in all secondary gap channels (5). [3] Reactor (1) according to claim 2, characterized by that the pressure control means comprise a pressure measuring device for measuring the pressure in the pressure vessel (18) and a secondary pressure measuring device for measuring the pressure in at least one of the secondary gap channels (5), and / or that the pressure control means comprise a secondary differential pressure measuring device for measuring the pressure difference between the pressure in the pressure vessel (18) and the pressure in at least one of the secondary gap channels (5). [4] Reactor (1) according to one of the preceding claims, characterized bythat in at least one of the secondary cracking channels (5), preferably in all secondary cracking channels (5), a catalyst material for an endothermic reaction, in particular a catalyst material for a hydrogen release reaction, in particular for an NH3 cracking or a methanol dehydrogenation or a methanol reforming or a DME reforming or a methane steam reforming or an LPG reforming or a butane or propane dehydrogenation, is provided. [5] Reactor (1) according to one of the preceding claims, characterized bythat the plate heat exchanger (2) comprises a preferably electrical heating device, in particular, wherein one or more plates (3) of the plate heat exchanger (2) can preferably be heated electrically by means of the heating device, and / or that a heating device arranged outside the pressure vessel (18) is provided, by means of which heating device the secondary medium, which can be supplied to the secondary gap channels (5) by means of the secondary fluid supply means, can be heated. [6] Reactor (1) according to one of the preceding claims, characterized by that the catalyst material provided in the primary gap channel(s) (4) comprises at least one noble metal, in particular platinum and / or palladium, in particular platinum provided on an aluminum oxide support. [7] Reactor (1) according to one of the preceding claims, characterized bythat the primary gap channels (4) and / or the secondary gap channels (5) are provided with stabilizing elements, in particular stabilizing webs. [8] Reactor (1) according to one of the preceding claims, characterized by that the pressure vessel (18) is provided on the inside with an insulating layer made of a thermally insulating material, and / or that the pressure vessel (18) comprises steel, in particular an outer shell made of steel, and / or that a leakage sensor is provided for monitoring the plate heat exchanger (2), wherein the leakage sensor is preferably arranged within the pressure vessel (18). [9] Reactor (1) according to one of the preceding claims, characterized bythat the plate heat exchanger (2) is provided on the outside with an insulating layer made of a thermally insulating material, and / or that the plates (3) of the plate heat exchanger (2) are at least substantially rectangular and / or have a structured surface on at least one side. [10] Reactor (1) according to one of the preceding claims, characterized by that the primary gap channels (4) and the secondary gap channels (5) are not fluidically connected to one another, and / or that the primary gap channels (4) and the secondary gap channels (5) are arranged alternately. [11] Reactor (1) according to one of the preceding claims, characterized bythat a pressure fluid circuit (21) is provided, via which pressure fluid can be discharged from the pressure vessel (18) and fed back into the pressure vessel (18), and / or that a pressure fluid temperature control device is provided for cooling and / or heating the pressure fluid, preferably, wherein the pressure fluid temperature control device is designed and arranged in such a way that pressure fluid can be cooled and / or heated by means of it before entering the pressure vessel (18) and / or after exiting the pressure vessel (18). [12] Use of a reactor (1) according to one of the preceding claims for a catalytic oxidation reaction, in particular for a catalytic oxidation reaction of hydrogen, preferably a catalytic combustion of hydrogen with oxygen, and / or for a hydrogen release reaction, in particular for an NH3 cracking or a methanol reforming or a DME reforming or a methane steam reforming or an LPG reforming or a butane or propane dehydrogenation, and / or for heating water to saturated steam or superheated steam. [13] Method for operating a reactor (1) according to one of claims 1 to 11, comprising the steps - a primary fluid is supplied to at least one primary gap channel (4), preferably to all primary gap channels (4), and an exothermic reaction, in particular an oxidation reaction of hydrogen, preferably a catalytic combustion of hydrogen with oxygen, is carried out in the at least one primary gap channel (4), preferably in all primary gap channels (4), - a secondary fluid is supplied to at least one secondary gap channel (5), preferably to all secondary gap channels (5), - a pressurized fluid, in particular a pressurized gas, is supplied to the pressure vessel (18), wherein the pressurized fluid comprises or is provided by N2 and / or liquid water and / or water vapor and / or air. [14] Method according to claim 13, characterized bythat the reactor (1) is operated in such a way that the pressure in the pressure vessel (18) is at most 20%, in particular at most 10%, preferably at most 5%, particularly preferably at most 1% above or below the pressure in at least one of the secondary gap channels (5), preferably in all of the secondary gap channels (5), and / or that the reactor (1) is operated in such a way that the pressure in the pressure vessel (18) is at most 5 bar, in particular at most 1 bar, preferably at most 100 mbar above or below the pressure in at least one of the secondary gap channels (5), preferably in all of the secondary gap channels (5). [15] Method according to one of claims 13 or 14, characterized by that the pressure fluid is at least partially repeatedly or continuously exchanged, and / or that pressure fluid removed from the pressure vessel (18) is fed back into the pressure vessel (18), preferably following cooling and / or heating. [16] Method according to one of claims 13 to 15, characterized by that a primary fluid is supplied to the at least one primary gap channel (4) which comprises or is provided by a mixture of hydrogen and oxygen, preferably, wherein a primary fluid is supplied which is located outside the explosive region, and / or that a primary fluid is supplied to the at least one primary gap channel (4) which comprises a retentate originating in particular from a product processing. [17] Method according to one of claims 13 to 16, characterized by that in particular boiling methanol or in particular boiling water or a thermal oil or a salt melt or a gas, in particular compressed air, is supplied to the at least one secondary gap channel (5) as a secondary fluid. [18] Method according to one of claims 13 to 17, characterized bythat a reaction fluid for an endothermic reaction is supplied to the at least one secondary cracking channel (5) as a secondary fluid, and in the at least one secondary cracking channel (5) an endothermic reaction, in particular a hydrogen release reaction, preferably an NH3 cracking or a DME reforming or a methane steam reforming or a methanol reforming or an LPG reforming or a butane or propane dehydrogenation, is carried out. [19] Method according to claim 18, characterized by that in a start-up phase the plate heat exchanger (2) is heated to provide heat for the endothermic reaction. [20] Method according to claim 18 or 19, characterized by that a methanol reforming is carried out in the at least one secondary splitting channel (5) and that a catalytic oxidation reaction of a part of the product stream is carried out in the at least one primary splitting channel (4). [21] Method according to one of claims 13 to 20, characterized by that the secondary fluid is evaporated and / or superheated as a result of the absorption of the heat released during the exothermic reaction in the at least one primary gap channel (4), or that heated secondary fluid is used to generate and / or superheat steam. [22] Method according to one of claims 13 to 21, characterized by that saturated steam or superheated steam is generated in at least one of the secondary gap channels (5), preferably in all secondary gap channels (5).

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