Reactor for carrying out exothermic reactions, and use and method for operating such a reactor

Abstract

The present invention relates to a reactor (1) comprising: a plate heat exchanger (2) having a plurality of adjacent plates (3) between which gap channels (4, 5) are defined, said gap channels (4, 5) being divided into a plurality of fluidically interconnected primary gap channels (4) and a plurality of 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) that encloses the plate heat exchanger (2); and pressure fluid supply means (19) that are designed to supply a pressure fluid to the pressure vessel (18).

Description

[0001] DESCRIPTION

[0002] Reactor for carrying out exothermic reactions, as well as use and methods for operating such a reactor

[0003] The invention relates to a reactor for carrying out exothermic reactions. Furthermore, the invention relates to the use and a method for operating such a reactor.

[0004] 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, for example, water (vapor) or thermal oil.

[0005] Specifically, heat sinks can be endothermic reactions and heat sources exothermic reactions. Specific heat sinks are catalyzed, endothermic reactions. The applicant is aware that the following reactor types are sometimes used for such reactions:

[0006] - Heated tube bundle reactors

[0007] - Adiabatic beds with intermediate heating (horde reactor)

[0008] - Heated fluidized bed reactors

[0009] Plate reactors are also known from the prior art. These offer the advantage of a large exchange surface area. However, due to their rectangular shape, they are only conditionally pressure-stable. Chemical reactions, e.g., endothermic reactions, often take place under overpressure, which can pose a significant challenge to the reactors used. Examples of endothermic reactions that take place under overpressure, including reactor types known to the applicant, are:

[0010] - Ammonia cracking - Tray and tube bundle reactor

[0011] - Methane steam reforming - Tube bundle reactor

[0012] - Methanol steam reforming - Tube bundle reactor

[0013] - Propane and butane dehydrogenation (Oleflex) - Tray reactor

[0014] The aforementioned reactor concepts all have disadvantages. In adiabatic beds with intercooling, the catalyst beds are generally very large because the catalyst is not utilized efficiently. Furthermore, a comparatively large amount of equipment is required for the intermediate heat exchangers. While heated tube bundle reactors offer comparatively good catalyst utilization, they are generally very expensive because their size scales with the number of tubes.

[0015] In the field of electrolysis and fuel cell technology, electrolysis and fuel cell stacks are known that are arranged in a pressure vessel. A high-pressure electrolysis cell is described, for example, in JP 5 524 227 B2.

[0016] US Patent 6,153,083 A discloses an electrolyzer for the electrolysis of water into hydrogen and oxygen, comprising a number of electrolysis cells, each containing an anode and a cathode, connected in series within a cell block enclosed in a pressure vessel. US Patent 6,689,499 B2 discloses pressurized fuel cell generator modules protected by purge gas.

[0017] The JP 3 845 780 B2 discloses atmospheric and pressurized SOFC power generation systems.

[0018] It is therefore an object of the present invention to provide an alternative reactor for carrying out exothermic reactions which avoids or at least reduces the aforementioned disadvantages and can be manufactured with comparatively little effort. It is further an object of the invention to provide a method for operating such a reactor.

[0019] The first-mentioned problem is solved 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 plates oriented at least substantially parallel to each other, between which gap channels are defined, wherein the gap channels are divided into several primary gap channels that are fluidically connected, in particular flow-wise in parallel, and several secondary gap channels that are fluidically connected, in particular flow-wise in parallel, wherein a catalyst material for an exothermic reaction, in particular for a catalytic oxidation reaction, preferably for a catalytic oxidation reaction of hydrogen, and particularly preferably a catalytic combustion of hydrogen with oxygen, is provided in at least one of the primary gap channels, preferably in all primary gap channels.and wherein primary fluid supply means are provided for supplying a primary fluid to the primary slotted channels and secondary fluid supply means for supplying a secondary fluid to the secondary slotted channels, a pressure vessel surrounding the plate heat exchanger, pressure fluid supply means configured to supply a pressure fluid to the pressure vessel and, in particular, to generate an increased pressure of at least 2 bar, in particular at least 5 bar, preferably at least 10 bar, and especially preferably at least 20 bar, in the pressure vessel.

[0020] The second problem is solved according to the invention by a method for operating a reactor according to the invention, comprising the steps

[0021] - at least one primary slit channel, preferably all primary slit channels, is supplied with a primary fluid 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 slit channel, preferably in all primary slit channels,

[0022] - at least one secondary slit channel, preferably all secondary slit channels, is supplied with a secondary fluid,

[0023] - a pressure fluid, in particular a pressure gas, is supplied to the pressure vessel, preferably wherein the pressure fluid comprises or is provided by N2 and / or liquid water and / or water vapor and / or air.

[0024] In other words, the present invention proposes the use of a plate heat exchanger for carrying out chemical reactions. A plate heat exchanger, in a well-known manner, comprises a plurality of plates, with a gap channel formed between each pair of adjacent plates. The gap channels are generally divided into two groups, and the gap channels of one group typically alternate with those of the other group. The two groups of gap channels are fluidically separated from each other but thermally coupled. In the conventional operation of a plate heat exchanger, for example, the gap channels of both groups are traversed by a heat transfer medium, and an efficient exchange of thermal energy takes place between the heat transfer media.

[0025] According to the invention, selected slit channels, and in particular at least a group of the slit channels, are used to carry out or operate an exothermic reaction within them. These slit channels provided or used for the exothermic reaction are referred to herein as primary slit channels. According to the invention, a catalyst material is provided in the primary slit 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 slit channels for the reaction. This can also be referred to as the reaction fluid.

[0026] The other group of slit channels, referred to here as secondary slit channels, can be used, for example, to dissipate heat released during the exothermic reaction. In this configuration, the primary slit channels can also be described as reaction slit channels, and the secondary slit channels as cooling slit channels. A secondary fluid is supplied to the secondary slit channels. If this fluid is used for heat dissipation, it can be said to serve as a cooling medium. This can be a "classic" heat transfer fluid, such as water or thermal oil, which is heated by the heat from the exothermic oxidation reaction. For example, water can be heated to saturated steam or superheated steam. 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.Cooling is achieved via the secondary side by means of an endothermic reaction.

[0027] Optionally, a catalyst material can also be provided in the secondary slit channels. Any catalyst material present in the secondary slit channels, which can also be referred to as "secondary catalyst material" for differentiation, may differ from the catalyst material in the primary slit channels.

[0028] Within the scope of the present invention, various exothermic and endothermic reactions can be combined. Alternatively or additionally, secondary slit channels can be used as heating / cooling channels and a heat transfer fluid can flow through them.

[0029] The reactor according to the invention is in particular a thermocatalytic reactor.

[0030] 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, no electrolytic reactions are carried out in the primary or secondary slit channels within the framework of the process according to the invention.

[0031] Advantageously, the primary and secondary slit channels are not fluidically connected. In the reactor according to the invention, it has also proven particularly advantageous to arrange the primary and secondary slit channels alternately, in other words, a primary slit channel alternates with a secondary slit channel. This allows, for example, particularly efficient cooling of an exothermic reaction on the primary side.

[0032] According to the invention, the plate heat exchanger is further provided for in a pressure vessel in which an elevated pressure is present 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 small pressure differential to the outside, in other words, compared to the pressurized interior of the pressure vessel. The plate heat exchanger can therefore be of a comparatively simple design. High pressures and temperatures can prevail in the secondary and / or primary channels during operation without the need for complex sealing of the plate heat exchanger or the secondary and / or primary channels.In particular, it can be assumed 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.

[0033] The present invention combines several advantages. On the one hand, the reactor according to the invention can be manufactured relatively cost-effectively. At the same time, it offers a high degree of safety. It provides good thermal integration, especially compared to adiabatic beds with intercooling. It offers high load flexibility and can also handle rapid load changes. This is particularly advantageous because cooling can be used instead of adiabatic beds. Furthermore, the reactor according to the invention can be started up relatively quickly. For example, the secondary fluid can also be used for preheating during the start-up phase, which will be discussed in more detail below.

[0034] In a preferred embodiment, the pressure vessel has a shape that is at least substantially cylindrical, and in particular circular cylindrical. It may have a (circular) hollow cylindrical shell that is closed at both ends. It may have rounded, and in particular convex, outwardly 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 manufacturing on the other, while still maintaining very good pressure resistance.

[0035] The pressure vessel is preferably designed to be explosion-proof, so that a particularly high level of safety can be achieved.

[0036] The pressure vessel can be provided internally with an insulating layer made of a thermally insulating material. Examples of thermally insulating materials include fireclay bricks, glass fabric, and / or ceramic fabric, such as polycrystalline mullite / aluminum oxide wool (PCW). Alternatively or additionally, the pressure vessel can be made of steel, in particular an outer shell made of steel. If the pressure vessel includes an internal thermal insulating layer, it can be prevented that its outer shell heats up to high temperatures during operation. This makes it possible to use an outer shell made of less temperature-resistant materials, in particular cost-effective steels that can withstand, for example, temperatures of only 250°C, preferably 220°C, and most preferably 100°C.

[0037] A leakage sensor can also be provided to monitor the plate heat exchanger. This sensor allows the plate heat exchanger to be monitored for leaks. The leakage sensor is preferably located inside the pressure vessel. If the pressure vessel is filled with inert gas, it is advantageous to monitor for a component from the plate heat exchanger that is not similar to the inert gas. For example, if the pressure vessel is filled with dry air or nitrogen, and high-pressure steam is generated on the secondary side of the plate heat exchanger, the humidity in the pressure vessel can be monitored. If, for example, endothermic methanol vapor reforming takes place and nitrogen (N₂) is supplied to the pressure vessel as a pressurized gas (i.e., it is purged with N₂), the leakage sensor is advantageously used to test for or monitor for hydrogen (H₂), carbon dioxide (CO₂), or hydrogen (H₂O).

[0038] In principle, various catalyst materials can be used within the scope of the present invention.

[0039] The catalyst material provided in the primary slit channel(s) can, for example, comprise at least one precious metal, in particular platinum and / or palladium, preferably platinum provided on a metal oxide support, in particular platinum provided on an aluminum oxide support.

[0040] As noted, in further development, a catalyst material for an endothermic reaction, in particular a catalyst material for a hydrogen release reaction, especially 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, for example, comprise copper and / or palladium and / or zinc.

[0041] The catalyst material provided in the primary slotted channel(s) and any catalyst material provided in the secondary slotted channels may be located on a support material. The (respective) catalyst material or the support material thereof may, for example, be granular. It may be in the form of pellets, or pellets containing the catalyst material may be provided in the primary slotted channels. Alternatively or additionally, the catalyst material may also be in the form of at least one coating, for example, obtained by a washcoat. For example, plates of the plate heat exchanger may be coated with the catalyst material or a coating material containing the catalyst material. One or more insert plates may also be arranged in the primary slotted channels and / or in the secondary slotted channels.These components can consist of the catalyst material or be coated with it, for example by a washcoat, which can simplify manufacturing. It is also possible for the catalyst material to be present in the form of catalytically active structures. For example, catalytically active networks can be incorporated into the primary and / or secondary slit channels.

[0042] In a particularly preferred embodiment, a catalytic oxidation reaction is carried out in the primary slit channel(s). This can be an oxidation reaction of hydrogen, preferably a catalytic combustion of hydrogen with oxygen. The primary slit channel(s) preferably comprise a catalyst material for such a reaction.

[0043] It may be true that:

[0044] H2(g) + 1 / 202(g) -> H20(g) AH° = -242 kJ moM

[0045] A combustion mixture comprising a gaseous fuel and a gaseous oxidizing agent can be supplied as the primary fluid to at least one primary slit channel.

[0046] A catalytic oxidation of hydrogen takes place in a particularly advantageous embodiment under the conditions described in DE 102023200 245 B3.

[0047] In particular, a primary fluid comprising or consisting of a mixture of hydrogen and oxygen is supplied to the at least one primary slit channel, preferably wherein the primary fluid supplied is located outside the explosive range.

[0048] The oxygen concentration of the primary fluid is expediently located below the limiting oxygen concentration.

[0049] The explosive range is the range of mixing ratios of the primary fluid's components in which the primary fluid is explosive. Advantageously, the primary fluid is 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 a mixture is no longer explosive. There is insufficient oxygen to allow an explosion. Thus, a flame independent of an ignition source can no longer propagate independently. In particular, no explosive primary fluid is present at any point in the process according to the invention. How this is achieved technically 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 way. In addition, the combustion process is particularly efficient. Furthermore, no NOx emissions are produced.

[0050] In an advantageous embodiment, water can be heated to saturated or superheated steam by means of the exothermic reaction taking place in the primary slit channels, in particular the catalytic oxidation reaction of hydrogen. In this case, liquid water is supplied to the secondary slit channel(s) as the secondary fluid and evaporates, absorbing heat from the exothermic reaction taking place in the primary slit channels – for example, the catalytic oxidation reaction of hydrogen. A pressure of, for example, 165 bar can be present in the secondary slit channels, and liquid water at 340°C can be supplied to the secondary slit channels as the secondary fluid. Preferably, a pressure of at least a similar pressure, and in particular also a pressure of 165 bar, is present in the pressure vessel. A similar pressure, or a different pressure, such as atmospheric pressure, can also be present in the primary slit channels.

[0051] It is also possible that a retentate stream, particularly one originating from product processing, is used as the primary fluid or is a component of the primary fluid. In an advantageous embodiment, it can be provided that a primary fluid comprising a retentate or a retentate stream, particularly one originating from product processing, is supplied to the at least one primary slit channel.

[0052] Another preferred embodiment is characterized in that methanol reforming is carried out in the at least one secondary slit channel and a catalytic oxidation reaction of a portion of the product stream exiting the at least one secondary slit channel is carried out in the at least one primary slit channel. This combination of an endothermic reaction on the secondary side and an exothermic reaction on the primary side has proven to be particularly suitable within the scope of the present invention.

[0053] This may apply in particular:

[0054] CH3OH + H2O -> CO2 + 3 H2 AH° = +49.7 kJ mol-1

[0055] In the secondary slit channels, where the methanol reforming takes place, there is a methanol reforming catalyst which includes or consists of, for example, Cu or Pd / Zn.

[0056] In the primary slit channels, catalytic oxidation takes place for heating purposes. Preferably, a portion of the product stream, consisting primarily of hydrogen (and CO2) and containing smaller amounts of methanol, H2O, and CO, is used for this purpose. The hydrogen, as a valuable product, can be further utilized, for example, in chemical reactions for steel production or power generation. A separation process typically occurs, such as membrane separation or pressure swing adsorption, yielding a retentate (low 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) that can be used for heating. Preferably, the retentate or a portion thereof is used for heating.In other words, it can be provided that the retentate from a separation process of the product stream, for example from a membrane separation or pressure swing adsorption, is supplied to at least one primary slit channel as a primary fluid or as a component of the primary fluid.

[0057] 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, thereby providing the heat required for the endothermic reaction on the secondary side.

[0058] 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 slit channels).

[0059] The reactor according to the invention can include pressure control means which are designed and / or configured in such a way that 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 slotted channels, preferably in all secondary slotted channels, is adjustable, preferably controllable.

[0060] In an advantageous further development of the method according to the invention, it is provided that the reactor is operated such that the pressure in the pressure vessel lies a maximum of 20%, in particular a maximum of 10%, preferably a maximum of 5%, and most preferably a maximum of 1% above or below the pressure in at least one of the secondary slotted channels, preferably in all secondary slotted channels, which has proven to be particularly suitable. Alternatively or additionally, the reactor can be operated such that the pressure in the pressure vessel lies a maximum of 5 bar, in particular a maximum of 1 bar, and preferably a maximum of 100 mbar above or below the pressure in at least one of the secondary slotted channels, preferably in all secondary slotted channels. In other words, when setting or adjusting the pressure in the pressure vessel, the pressure in the secondary slotted channels can be adjusted to the maximum pressure in the secondary slotted channels.The regulation of a maximum pressure difference between the interior of the pressure vessel and the pressure in one or more secondary slotted channels can be based on a percentage difference and / or absolute deviations.

[0061] Pressure control means of the reactor according to the invention can be designed and / or configured to achieve this.

[0062] In other words, the pressure in the pressure vessel is then the same as, or at least very similar to, the pressure in one or more secondary air channels. The pressure of the compressed gas can be adjusted during operation to match the pressure in the secondary air channel(s). The pressure control devices can be designed and / or configured accordingly.

[0063] If pressure control means are present, these can alternatively or additionally be designed and / or arranged in such a way that the pressure difference prevailing during the operation of the reactor between the pressure in at least one of the primary slotted channels, preferably in all primary slotted channels and the pressure in at least one of the secondary slotted channels, preferably in all secondary slotted channels, can be adjusted, preferably controlled.

[0064] The reactor can further be operated such that the pressure in at least one of the secondary fission channels, preferably the pressure in all secondary fission channels, is a maximum of 20%, in particular a maximum of 10%, preferably a maximum of 5%, and most preferably a maximum of 1% above or below the pressure in at least one of the primary fission channels, preferably in all primary fission channels. Alternatively or additionally, the reactor can be operated such that the pressure in at least one of the secondary fission channels, preferably the pressure in all secondary fission channels, is a maximum of 5 bar, in particular a maximum of 1 bar, and more preferably a maximum of 100 mbar above or below the pressure in at least one of the primary fission channels, preferably in all primary fission channels.

[0065] Pressure control means of the reactor according to the invention can be designed and / or configured to achieve this.

[0066] 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.

[0067] However, a pressure difference can also exist, and (significantly) different pressures are also possible in principle. The secondary and / or primary slot channels, or the plates defining the secondary and / or primary slot channels, can then be welded together, or suitable seals and sufficient contact pressure of the plates can be implemented to allow for higher pressure differences.

[0068] It is also possible for the primary and / or secondary slot channels to be provided with stabilizing elements, in particular stabilizing ribs. These stabilizing elements can increase stability. Especially in applications where larger pressure differences between primary and secondary slot channels occur (or may occur), it can be advantageous to reinforce the slot channels accordingly. Stabilizing elements, for example in the form of stabilizing ribs, can extend between two adjacent plates and be supported by the adjacent plates.

[0069] In the event that a significant pressure difference between the primary and secondary channels occurs or is intended to occur during operation, for example, a pressure difference of more than 5 bar, or possibly even considerably more than 5 bar, the sealing of the plate heat exchanger can be specifically designed so 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, they can be arranged so 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, is pressed against at least one other element of the plate heat exchanger during operation.

[0070] 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 slotted channels can be adjusted, preferably regulated. Alternatively or additionally, the pressure in the primary slotted channels can be adjusted, preferably regulated, by means of the control device.

[0071] As a rule, the pressure in the secondary channel(s) and the pressure in the secondary fluid supply to the secondary channels and / or in the secondary fluid discharge from the secondary channels are nearly identical. This is particularly true if no valve or similar device is installed between the plate heat exchanger or its secondary channels and at least one supply or discharge line. The same applies to the primary channels and the pressure vessel and at least one supply or discharge line. Here, too, the pressure is nearly identical, especially if no valve or similar device is installed between the primary channels or the pressure vessel and a supply or discharge line.

[0072] Accordingly, the optionally available pressure control means can be designed and / or configured in such a way that the pressure difference prevailing during operation of the device between the pressure in the pressure vessel and / or the pressure in at least one line upstream or downstream of the pressure vessel on the one hand, and the pressure in at least one of the secondary slot channels, preferably in all secondary slot channels, and / or in at least one line upstream or downstream of the secondary slot channels on the other hand, is adjustable, preferably controllable.

[0073] A pressure measuring device may also be provided for measuring the pressure in the pressure vessel and / or in at least one, preferably exactly one, line upstream of the pressure vessel. Alternatively or additionally, a pressure measuring device may be provided for measuring the pressure in at least one, preferably exactly one, line downstream of the pressure vessel. This may, for example, be a pressure measuring device for measuring the pressure in a pressure inlet line and / or for measuring the pressure in a pressure outlet line through which pressure fluid can be supplied to or removed from the pressure vessel.

[0074] Furthermore, at least one secondary pressure measuring device can be provided for measuring the pressure in one – or even several, possibly all – secondary slotted channels. Alternatively or additionally, a secondary pressure measuring device can be provided for measuring the pressure in at least one, preferably exactly one, line upstream of the secondary slotted channels and / or the pressure in at least one, preferably exactly one, line downstream of the secondary slotted channels.

[0075] Alternatively or additionally, the reactor according to the invention can include a secondary differential pressure measuring device for measuring the pressure difference between the pressure in the pressure vessel and / or in at least one, preferably exactly one, line upstream of the pressure vessel and the pressure in at least one of the secondary slotted channels. If a secondary differential pressure measuring device is provided, it can alternatively or additionally be configured to measure the pressure difference between the pressure in the pressure vessel and / or in at least one line upstream of it on the one hand, and the pressure in at least one line upstream of the secondary slotted channels and / or in at least one line downstream of the secondary slotted channels on the other.

[0076] At least one primary pressure measuring device can also be provided for measuring the pressure in one – or even several, possibly all – primary slotted channels. Alternatively or additionally, a primary pressure measuring device can be provided for measuring the pressure in at least one, preferably exactly one, line upstream of the primary slotted channels and / or the pressure in at least one, preferably exactly one, line downstream of the primary slotted channels.

[0077] Alternatively or additionally, the reactor according to the invention can include a primary differential pressure measuring device for measuring the pressure difference between the pressure in the pressure vessel and / or in at least one line upstream of the pressure vessel and / or in at least one line downstream of the pressure vessel on the one hand, and the pressure in at least one of the primary slotted channels on the other. If a primary differential pressure measuring device is provided, it can alternatively or additionally be configured to measure the pressure difference between the pressure in the pressure vessel or in at least one line upstream of it and / or in at least one line downstream of it on the one hand, and the pressure in at least one line upstream of the primary slotted channels and / or in at least one line downstream of the primary slotted channels on the other.

[0078] The line upstream of the secondary slotted channel(s), in which the pressure can be measured alternatively or additionally, can be, for example, a secondary inlet line and / or a secondary distribution channel or one of several arms of a secondary distribution channel. The line is fluidically connected upstream of the secondary slotted channel(s) and can be directly connected to one or more of the secondary slotted channels, or via one or more other lines.

[0079] Similarly, the line downstream of the secondary slotted channel(s), in which the pressure can be measured alternatively or additionally, can be, for example, a secondary outlet line and / or a secondary collector channel or one of several arms of a secondary collector channel. The line is fluidically connected downstream of the secondary slotted channel(s) and can be directly connected to one or more of the secondary slotted channels, or via one or more further lines.

[0080] Furthermore, the line upstream of the primary slotted channels, in which the pressure can be measured alternatively or additionally, can be, for example, a primary inlet line and / or a primary distribution channel or one of several branches of a primary distribution channel. The line is fluidically connected upstream of the primary slotted channel(s) and can be directly connected to one or more of the primary slotted channels, or via one or more other lines.

[0081] The line downstream of the primary slotted channels, in which the pressure can be measured alternatively or additionally, can be, for example, a primary outlet line and / or a primary collector channel or one of several arms of a primary collector channel. The line is fluidically connected downstream of the primary slotted channel(s) and can be directly connected to one or more of the primary slotted channels, or via one or more other lines.

[0082] The line upstream of the pressure vessel can be, for example, a pressure inlet line, and the line downstream of the pressure vessel can be, for example, a pressure outlet line.

[0083] 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 can be part of the pressure control means of the reactor.

[0084] 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 can also be connected to a control device for the pressure control means. Depending on the measured pressure (differential) values, at least one valve and / or at least one pump and / or at least one compressor can be controlled, for example, to achieve the desired pressure. The pressure fluid supply means, which can include 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 for these.

[0085] It has also proven particularly advantageous if the pressure control means, in particular a control device thereof, are designed and / or configured such that the pressure in the pressure vessel and / or in at least one, preferably exactly one, line upstream or downstream of the pressure vessel can be adjusted, in particular regulated, as a function of the pressure in at least one of the secondary slotted channels and / or in at least one, preferably exactly one, line upstream or downstream of the secondary slotted channels. Alternatively or additionally, it can be provided that the pressure control means, in particular a control device thereof, are designed and / or configured such that the pressure in the pressure vessel and / or in at least one line upstream or downstream of the pressure vessel can be adjusted, in particular regulated, as a function of the pressure difference between the pressure in the pressure vessel and / or in at least one upstream or downstream line.The pressure in the downstream line on the one hand and in at least one of the secondary slot channels and / or in at least one, preferably exactly one, line upstream or downstream of the secondary slot channels on the other hand is adjustable, in particular controllable.

[0086] Alternatively or additionally, the pressure control means, in particular a control device thereof, can be designed and / or configured such that the pressure in at least one of the primary slotted channels and / or in at least one, preferably exactly one, line upstream or downstream of the primary slotted channels can be adjusted, in particular regulated, depending on the pressure in at least one of the secondary slotted channels and / or in at least one, preferably exactly one, line upstream or downstream of the secondary slotted channels. The pressure control means, in particular a control device thereof, can also be designed and / or configured such that the pressure in at least one of the primary slotted channels and / or in at least one, preferably exactly one, line upstream or downstream of the primary slotted channels can be adjusted, in particular regulated, depending on the pressure in at least one of the secondary slotted channels and / or in at least one, preferably exactly one, line upstream or downstream of the secondary slotted channels.downstream line, depending on the pressure difference between the pressure in the pressure vessel and / or in at least one, preferably exactly one, line upstream or downstream of the pressure vessel on the one hand and the pressure in at least one of the primary slot channels and / or in at least one, preferably exactly one, line upstream or downstream of the primary slot channels on the other hand, is adjustable, in particular controllable.

[0087] For example, the control device of the pressure control means can be conveniently connected to the primary fluid and / or the secondary fluid supply means.

[0088] The control device may also be designed and / or configured to obtain maximum pressure deviations in the aforementioned areas.

[0089] 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 advantageous. Similarly, 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 comprise 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 can each comprise at least one compressor and / or at least one pump and / or at least one valve, this is by no means a requirement.In the simplest case, these can each be provided by just a supply line or an inlet.

[0090] The pressure fluid supplied to the pressure vessel may, for example, include or be composed of N2 and / or liquid water and / or water vapor and / or air.

[0091] It should be noted that, in a preferred further development, the primary fluid is preheated before entering the primary fluid channel(s), for example by means of a heat exchanger provided for primary fluid preheating.

[0092] In an advantageous embodiment, the pressurized fluid can further be temperature-controlled, in particular heated or cooled. The reactor according to the invention can accordingly include a pressurized fluid temperature control device for temperature control of the pressurized fluid. It can be provided that the pressurized fluid is cooled and / or heated before entering the pressure vessel and / or after exiting the pressure vessel. The pressurized fluid temperature control device, if present, can be designed and arranged accordingly.

[0093] Another advantageous embodiment is further characterized in that the pressure fluid is at least partially replaced 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 after cooling and / or heating.

[0094] The reactor according to the invention can comprise a pressurized fluid circuit, whereby pressurized fluid can be discharged from the pressure vessel and returned to the pressure vessel. It can be provided that at least one, preferably all, secondary 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 channels, can be designed accordingly in a further development, for example, by being made of a suitable material.

[0095] 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 is suitable for a temperature range of 130°C to 350°C, which corresponds approximately 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 a molten salt, which has proven particularly suitable for a temperature range of 400°C or higher, approximately in the range of 400°C to 650°C.

[0096] It is also possible to carry out an endothermic reaction on the secondary side of the plate heat exchanger, which has proven to be particularly advantageous. Accordingly, the reactor according to the invention can be advantageously 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 slotted channels, preferably in all secondary slotted channels.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 slit channel as a secondary fluid, and that an endothermic reaction, in particular a hydrogen release reaction, preferably ammonia cracking or DME reforming or methane steam reforming or LPG reforming or butane or propane dehydrogenation, is carried out in the at least one secondary slit channel. A hydrogen-rich compound can, for example, be supplied as a secondary fluid to the at least one secondary slit channel, preferably to all secondary slit channels.

[0097] During a start-up phase for initiating the endothermic process, or when electricity costs are low, the plate heat exchanger can preferably be heated electrically to provide heat for the endothermic reaction and to start or continue it, in particular a hydrogen release reaction.

[0098] The plate heat exchanger according to the invention can advantageously include a preferably electric heating device. For example, one or more plates of the plate heat exchanger can preferably be heated 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 crack channels during a start-up phase or when electricity costs are low.

[0099] It is also possible to supply a heated fluid or gas to at least one primary slot channel, preferably all primary slot channels, during a start-up phase in order to preheat the catalyst and initiate the endothermic reaction. This form of heating can be used as an alternative or in addition to electrical heating of the plate heat exchanger, for example, of its plates.

[0100] 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 incorporate heating elements for heating the secondary fluid. This eliminates the need for electric heating plates in the reactor.

[0101] Another advantageous embodiment of the invention is characterized in that the secondary fluid is evaporated and / or superheated as a result of absorbing the heat released during the exothermic reaction in the at least one primary slot channel. It is also possible to use heated secondary fluid 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 with the produced hydrogen subsequently being used to produce ammonia (NH3). Such a configuration has proven to be particularly energy-efficient. Accordingly, the reactor according to the invention can comprise at least one solid oxide electrolyzer cell.

[0102] Furthermore, it may be provided that at least one of the secondary slot channels is subdivided into several, preferably flow-technically parallel, partial secondary slot channels. Such a subdivision, so to speak into several "sub-secondary slot channels," may also be provided for all secondary slot channels. Alternatively or additionally, at least one of the secondary slot channels, or even all of them, may have a meandering course. If a subdivision into several "sub-secondary slot channels" is present, these may also be meandering.

[0103] It has also proven useful to connect the primary split channels via a primary distribution channel and a primary collector channel.

[0104] Alternatively or additionally, it can be provided in an analogous manner that the secondary split channels are connected to each other via a secondary distribution channel and a secondary collector channel.

[0105] Each plate can, for example, have four holes, particularly round ones, wherein the holes are located in identical positions in all plates and the holes of all plates are aligned, and each aligned hole forms a primary-secondary distribution or collector channel extending transversely through the plates and the defined gap channels between them, in particular a cylindrical channel. If four holes are provided in each plate, in particular a primary distribution channel and a primary collector channel as well as a secondary distribution channel and a secondary collector channel are formed or defined.

[0106] The holes are preferably located in the edge region of the plates. If the plates are rectangular, and in particular at least substantially rectangular or square, one of the holes can be located, for example, in or near each corner of each plate. A further advantageous embodiment of the invention is characterized in that the primary slotted channels of the plate heat exchanger are connected to a primary inlet line, and a primary outlet line, which is particularly central. Similarly, the secondary slotted channels can be connected to a secondary inlet line, and a secondary outlet line, which is particularly central.

[0107] The primary slit channels can be connected, for example, to a primary intake manifold via a primary distributor channel and to a primary exhaust manifold via a primary collector channel. Similarly, the secondary slit channels can be connected to a secondary intake manifold via a secondary distributor channel and to a secondary exhaust manifold via a secondary collector channel.

[0108] The plates of a plate heat exchanger will typically have the same shape, for example, all being at least approximately rectangular, and / or characterized by identical external dimensions. It is also possible that several, or even all, of the plates of the plate heat exchanger are identical in construction. The plates are preferably made of or comprise metal.

[0109] Alternatively or additionally, the plates have a structured surface or profile on at least one side. Advantageously, the at least one side with a structured surface or profile is a side that defines or limits a gap channel.

[0110] In an advantageous embodiment, the plate heat exchanger can be provided with an external insulating layer made of a thermally insulating material. This prevents excessive heating of the pressure vessel surrounding the plate heat exchanger during operation. The plate heat exchanger can also include a housing. In this case, the housing, in particular, can have an insulating layer made of a thermally insulating material.

[0111] 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 NH3 cracking or methanol reforming or DME reforming or methane steam reforming or LPG reforming or butane or propane dehydrogenation, and / or for heating water to saturated steam or superheated steam.

[0112] 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.

[0113] Regarding the embodiments of the invention, reference is also made to the dependent claims and to the following description with reference to the accompanying drawing. In the drawing: Figure 1 shows an embodiment of a reactor according to the invention in a purely schematic sectional view.

[0114] Figure 2 is a perspective exterior view of the reactor from Figure 1, and

[0115] Figure 3 shows another purely schematic sectional view of the reactor from Figure 1.

[0116] The same reference symbols are used in the figures for identical or similar components and elements.

[0117] Figure 1 shows a first embodiment of a reactor 1 according to the invention in a purely schematic sectional view. Figure 2 shows the reactor 1 in a perspective external view and Figure 3 another schematic sectional view.

[0118] Reactor 1 is designed to carry out exothermic reactions.

[0119] The reactor 1 comprises a plate heat exchanger 2 with a plurality of adjacent plates 3, in particular plates oriented at least substantially parallel to one another. In Figure 1, only a few of the plates 3 are designated by reference numeral 3 for illustrative purposes. In the embodiment shown here, the plates 3, which are made of metal, all have a rectangular outer contour and the same dimensions; in other words, they are all the same size. Between the plates 3, gap channels 4, 5 are defined, specifically, one gap channel 4, 5 between each pair of adjacent plates 3. The gap channels 4, 5 are divided into two groups: several primary gap channels 4, which are fluidically interconnected, specifically connected in parallel, and several secondary gap channels 5, which are fluidically interconnected, specifically connected in parallel.The slit channels 4 of one group, the primary slit channels 4, alternate with the slit channels 5 of the other group, the secondary slit channels 5. A primary slit channel 4 is therefore always located between two secondary slit channels 5, or – in the case of the primary slit channel 4 on the far left of the figure, at the edge – next to a secondary slit channel 5. Similarly, a secondary slit channel 5 is always located between two primary slit channels 4, or – in the case of the secondary slit channel 5 on the far right of the figure, at the edge – next to a primary slit channel 4.

[0120] Each of the primary slot channels 4 contains a catalyst material 6 for an exothermic reaction. In the highly simplified, purely schematic Figure 1, the catalyst material 6 is only indicated by way of example in some of the primary slot channels 4. Figure 1 schematically shows, by way of example, a granular catalyst material 6, and even then only over a section of the respective primary slot channel 4. It is understood that the primary slot channels 4 can be filled with, for example, a granular catalyst material 6 along their entire length. Alternatively or additionally, it is also possible that the plates 3 are coated with catalyst material 6 or with a coating material containing catalyst material 6. One or more insert plates can also be arranged in the primary slot channels 4, which consist of the catalyst material or are coated with the catalyst material, for example by a washcoat, which can simplify manufacturing.It is also possible that the catalyst material is present in the form of catalytically active structures. For example, catalytically active networks may be provided in the primary and / or secondary slit channels.

[0121] 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 recognizable in Figure 1, but is not shown again in Figure 2.

[0122] The present material is a catalyst material 6 for a catalytic oxidation reaction of hydrogen, in particular a catalytic combustion of hydrogen with oxygen. The oxidation reaction is: H₂(g) + 1 / 202(g) -> H20(g) AH° = -242 kJ mol 1

[0123] In the illustrated embodiment, a catalyst material 6 is provided in the primary slit channels 4, which comprises or is provided as platinum, specifically platinum on a metal oxide support. The same catalyst material 6 is present in all primary slit channels 4.

[0124] Reactor 1 further comprises primary fluid supply means 7 for supplying a primary fluid to the primary slot channels 4. In the illustrated example, the primary fluid supplied is a combustion mixture comprising a gaseous fuel and a gaseous oxidizer. 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 limiting oxygen concentration. The primary fluid can also be referred to as the reaction fluid or reaction gas. The primary fluid supply means 7 comprise at least one blower / compressor and / or at least one valve, which are not shown separately in the purely schematic Figure 1.

[0125] As can be seen in Figure 1, the primary slotted channels 4 are all fluidically connected on the inlet side to a central primary distribution channel 8, which in the illustrated embodiment is part of the primary fluid supply means 7. During operation, the primary fluid enters the primary distribution channel 8 via the central primary inlet line 9 of the primary fluid supply means 7, indicated by an arrow in Figure 1. The primary fluid supplied can be distributed to all primary slotted channels 4 via the primary distribution channel 8.

[0126] The reactor 1 also includes secondary fluid supply means 10 for supplying a secondary fluid to the secondary slot channels 5. The secondary fluid supply means 10 include at least one pump and / or at least one valve, which are not shown separately in the purely schematic figure 1.

[0127] The secondary slot channels 5 are – analogous to the primary slot channels 4 – all fluidically connected at their inlet side to a central secondary distribution channel 11, which in the illustrated embodiment is part 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.

[0128] On the outlet side of the primary slotted channels 4, a primary collector channel 13 is provided, in which fluid exiting from all primary slotted channels 4 is collected and can exit the plate heat exchanger 2 via a central primary outlet line 14. Similarly, on the outlet side of the secondary slotted channels 5, a secondary collector channel 15 is provided, in which fluid exiting from all secondary slotted channels 5 is collected and can exit the plate heat exchanger 2 via a central secondary outlet line 16.

[0129] The primary slot channels 4 and the secondary slot channels 5 are not fluidically connected.

[0130] In the embodiment shown here, the plate heat exchanger 2 has a cuboid housing 17, through the wall of which the inlet and outlet lines 9, 12, 14, 16 for the primary and secondary fluid extend.

[0131] It should be noted that in the schematic figure 1, the two distribution and collector channels 8, 11, 13, 15 are shown above and below the plates 3, respectively, for the sake of clarity. However, these channels can also extend through the plates 3, in particular by being defined by recesses provided in the plates 3. For example, each plate 3 can have four holes, especially round ones (not shown in the figure), with the holes being located at identical positions in all plates 3 and aligned. Each set of aligned holes forms a primary or secondary distribution channel 8, 11, 13, 15, extending transversely through the plates 3 and the gap channels 4, 5 defined between them, and being cylindrical in shape. This is known from conventional plate heat exchangers or those used in conventional applications. The connection of the respective distribution or collector channel 8, 11, 13, 15 with the associated gap channels orThe separation can then be achieved via gaskets (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 rectangular, as in the illustrated embodiment, one of the holes can be located in or near each corner.

[0132] 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 a molten salt, is used as the secondary fluid.

[0133] Reactor 1 also includes a pressure vessel 18 that surrounds 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 inside the pressure vessel 18.

[0134] The pressure vessel 18 comprises an outer shell made of cost-effective steel, which is provided on the inside with an insulating layer of a thermally insulating material. The thermal insulation ensures or contributes to the fact that the outer shell has a maximum operating temperature of 200°C, preferably a maximum of 70°C, which allows the use of cost-effective steels. It should be noted that, alternatively or additionally, the plate heat exchanger 2, e.g., its housing 17, can also be provided with an insulating layer of a thermally insulating material. The pressure vessel 18 is designed in two parts, a first part 18a and a second part 18b. The two parts 18a and 18b are detachably connected to each other by integrally formed flanges 18c and screws not visible in the figures.The plate heat exchanger 2 is held in the pressure vessel 18 by a support 18d, which is preferably attached to the flanges 18c, at a distance from the pressure vessel wall (see Figure 3). Depending on the length of the plate heat exchanger 2, additional supports can be provided, particularly in the pressure vessel section 18a. It should be noted that the two-part design of the pressure vessel 18 is not apparent in the purely schematic, simplified Figure 1.

[0135] Furthermore, pressure fluid supply means 19 are provided, which are configured 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 at least 5 bar, preferably at least 10 bar, and most preferably 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 not shown separately in schematic Figure 1.

[0136] The pressure vessel 18 and the pressure fluid supply means 19 enable the plate heat exchanger 2 to operate when the exothermic reaction is carried out on the primary side and, if applicable, an endothermic reaction is carried out on the secondary side, without or with only a small pressure difference, in particular between the secondary slotted 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.

[0137] It should be noted that in the schematic, highly simplified figure 1, the seals, which in particular prevent the escape of primary and secondary fluid into the pressure vessel 18 or the ingress of pressure fluid into the primary and secondary gap channels 4, 5, are not shown.

[0138] A pressure fluid, comprising nitrogen, water, steam, or air, can be supplied to the pressure vessel 18 by means of the pressure fluid supply means 19. Temperature control of the pressure fluid can be provided. The reactor 1 shown in Figure 1 comprises a pressure fluid circuit 21 with a pressure fluid temperature control device, which includes or is provided by means of a heat exchanger 22. Pressure gas can be drawn from the pressure vessel 18 via the pressure fluid circuit 21, cooled / heated by means of the pressure fluid temperature control device, in particular by means of the heat exchanger 22, and then returned to the pressure vessel 18. The circuit 21 also includes a compressor / pump 23. Additional cooling can be achieved via a circulated, cooled pressure fluid.

[0139] The pressure vessel 18 can also be equipped with a leakage sensor (not shown).

[0140] Pressure control means are provided which are designed and / or configured in such a way that the pressure difference prevailing during the operation of reactor 1 between the pressure in the pressure vessel 18 and the pressure in the secondary slotted channels 5 can be adjusted, preferably controlled.

[0141] 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. The control device 24 can also be used to adjust, preferably regulate, the pressure in the secondary slit channels 5. For this purpose, the control device 24 is expediently connected to the secondary fluid supply means 10 and the pressure fluid supply means 19, for example, compressors thereof.

[0142] Pressure measuring devices, such as pressure sensors, may be provided for measuring the pressure in the pressure vessel 18 and / or the pressure in at least one secondary slotted channel 5. Alternatively or additionally, a secondary differential pressure measuring device may 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 slotted channels 5. Alternatively or additionally, a pressure measuring device may be provided for measuring the pressure in at least one primary slotted channel 4. The pressure measuring devices and / or the secondary differential pressure measuring device may be part of the pressure control system. The control unit 24 may be connected to the pressure measuring devices and / or the differential pressure measuring device to enable control or regulation based on the measured pressure values.

[0143] It should be noted that, alternatively or additionally to pressure measurement in the pressure vessel 18 or at least one secondary channel 5, the pressure can also be measured in the supply line, specifically in at least one line upstream of the pressure vessel 18 or in at least one line upstream of one or more, or possibly all, secondary channels 5. By way of example, at least one pressure measuring device, e.g., at least one pressure sensor, is provided for measuring the pressure in the secondary inlet line 12 and / or the secondary distribution channel 11, for instance, in at least one of its multiple arms. Differential pressure measurement can also be performed in the supply line, specifically at least one line upstream of the pressure vessel 18 or at least one secondary channel 5.

[0144] Regarding the primary slotted channels 4, it can alternatively or additionally be the case that at least one pressure measuring device, e.g., at least one pressure sensor, is provided for the metrological measurement of the pressure in the primary inlet line 8 and / or the primary distribution channel 8, for example, in at least one of its several arms. Differential pressure measurement can also be based on the supply, specifically at least one line upstream of the pressure vessel 18 or at least one primary slotted channel 4 or secondary slotted channel 5.

[0145] Alternatively or additionally, pressure measurement can be performed in a feed line, or in at least one downstream line. For example, at least one pressure measuring device, such as at least one pressure sensor, can be provided for measuring the pressure in the secondary collector channel 15, for instance, in at least one of its multiple arms. Differential pressure measurement can also be performed in the outflow, specifically in at least one line downstream of the pressure vessel 18 or at least one secondary slotted channel 5.

[0146] The same applies to the primary slot channels 4. At least one pressure measuring device, e.g., at least one pressure sensor, can be provided for measuring the pressure in the primary outlet line 14 and / or the primary collector channel 13, for example, in at least one of its several arms. Differential pressure measurement can also be performed using the downstream line, specifically at least one line connected downstream of at least one primary slot channel 4 or secondary slot channel 5.

[0147] It goes without saying that other combinations of pressure measuring devices are also possible and the above is merely an example.

[0148] 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 activates in the event of excessive pressure (not shown in the figure). Pressure fluid can then be diverted via such a safety valve, for example, to a flare or safe location.

[0149] Furthermore, a vent valve J is provided for the plate heat exchanger 2.

[0150] During operation of reactor 1, the primary fluid is supplied to the primary slotted channels 4, in other words, the primary side of the plate heat exchanger 2, and water, for example, is supplied as the secondary fluid to the secondary slotted channels 5, i.e., the secondary side. Simultaneously, a pressurized fluid, in this case nitrogen or air, is supplied to the pressure vessel.

[0151] It should be noted that the primary or secondary fluid can be preheated before entering the primary slotted channels 4 or secondary slotted channels 5, respectively. Reactor 1 may include a heat exchanger for primary fluid preheating and / or secondary fluid preheating (not shown).

[0152] In the primary slotted channels 4, hydrogen is oxidized according to the equation above, releasing heat. Cooling occurs via the secondary side of the plate heat exchanger 2, through the water flowing in the secondary slotted channels 5. Specifically, the water in the secondary slotted 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 slotted channels 5, in liquid form at 340°C. Saturated steam or superheated steam at 350°C or more than 350°C exits the secondary outlet line 16. The catalytic oxidation of hydrogen in the primary slotted channels 4 preferably takes place under the conditions described in DE 10 2023 200 245 B3.

[0153] In the embodiment shown in Figure 1, additional cooling can be achieved via the cooled pressure fluid.

[0154] The pressure in the pressure vessel 18 is adjusted to the pressure in the secondary slotted channels 5 by means of the control device 24.

[0155] Specifically, the reactor 1 is operated such that the pressure in the pressure vessel 18 is controlled by the control device 24 by a maximum of 20%, in particular by a maximum of 10%, preferably by a maximum of 5%, and most preferably by a maximum of 1% above or below the pressure in the secondary slotted channels 5. In the 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 by a maximum of 1 bar, and preferably by a maximum of 100 mbar above or below the pressure in the secondary slotted channels 5. The control device 24 is designed and / or configured accordingly.

[0156] The primary side, specifically the primary slot channels 4, can be at the same or a similar pressure, or at a (significantly) different pressure, for example, atmospheric pressure. If the same or a similar pressure is desired, the reactor 1 can, for example, be operated such that the pressure in the primary slot channels 4 is a maximum of 20%, in particular a maximum of 10%, preferably a maximum of 5%, and most preferably a maximum of 1% above or below the pressure in the secondary slot channels 5. Specifically, the reactor 1 can be operated such that the pressure in the primary slot channels 4 is a maximum of 5 bar, in particular a maximum of 1 bar, and preferably a maximum of 100 mbar above or below the pressure in the secondary slot channels 5.

[0157] The control unit 24 is appropriately trained and / or configured.

[0158] In particular, if a plate heat exchanger 2 with a more elaborate seal and stabilizing struts is used, operation with significantly different pressures is also possible.

[0159] The leakage sensor of pressure vessel 18 monitors for a lack of gas. The leakage sensor detects a leak, in particular, between secondary gap channels 5 and pressure vessel 18 if the pressure in the secondary gap channel 5 is even slightly higher than in the pressure vessel 18.

[0160] Primary fluid exiting from the primary slot channels 4 on the outlet side after the reaction is collected in the primary collector channel 13 and can be routed via the primary outlet line 14 out of the plate heat exchanger 2 and the pressure vessel 18 and supplied to a desired use, e.g. heat recovery as described in DE 102023200245 B3.

[0161] Heated secondary fluid, in the form of saturated or superheated steam, exits from the secondary vent channels 5 on the outlet side. This saturated / superheated steam can also be used for a desired application.

[0162] 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 absorbing and dissipating the heat released during the exothermic reaction, in this case the catalytic oxidation reaction of hydrogen, in the primary slotted channels 4. If this is the case, a catalyst material for an endothermic reaction, e.g., a hydrogen release reaction, is advantageously provided in the secondary slotted channels 5 (not shown in Figure 1). In other words, not only the primary slotted channels 4 but also the secondary slotted channels 5 can then be filled with a catalyst material.

[0163] In this case, a reaction fluid for the endothermic reaction is supplied to the secondary slit 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 example, for a hydrogen release reaction, a hydrogen-rich compound would be supplied as the secondary fluid, and hydrogen would be released by absorbing heat from the reaction side.

[0164] As an example of a hydrogen release reaction carried out on the secondary side, methanol reforming may be mentioned. In this case, a methanol reforming catalyst material 6, comprising or consisting of Cu or Pd / Zn, is expediently arranged in the secondary slit channels 5.

[0165] It has proven particularly advantageous to perform methanol reforming in the secondary slit channels 5 and a catalytic oxidation reaction of a portion of the product stream in the primary slit channels 4. The product stream can consist predominantly of hydrogen (and CO2) and contain smaller amounts of methanol and CO. The retentate from a separation process of the product stream, e.g., from membrane separation or pressure swing adsorption, can be used as the primary fluid. Together with an oxidizing agent, such as 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.

[0166] The pressure in pressure vessel 18 is expediently set to a pressure of 20 bar (similar to the methanol reforming pressure prevailing in the secondary slotted channels 5 during operation) or deviating from this by a maximum of 20 bar. 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 slotted channels 4 can also correspond at least approximately to this pressure or even deviate from it more significantly, for example, to atmospheric pressure.

[0167] Other endothermic reactions, the execution of which on the secondary side has also proven to be particularly suitable as an alternative to methanol reforming, are

[0168] NH3 cracking

[0169] DME Reforming

[0170] Methane steam reforming

[0171] LPG reform

[0172] Butane / propane dehydration

[0173] In all these reactions, a retentate stream from the product preparation can be used to provide heat through oxidation (via the primary side). The catalytic oxidation of hydrogen in the primary slot channels 4 can take place in all cases under the conditions described in DE 10 2023 200 245 B3. 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 externally.

[0174] If an endothermic reaction, such as an endothermic hydrogen release reaction, is used on the secondary side, a hydrogen-rich compound can be supplied to the secondary slit channels 5 as a secondary fluid. In this case, the hydrogen is released in the secondary slit channels 5, which are equipped with a suitable catalyst material for the endothermic reaction. Hydrogen and a hydrogen-poor compound exit the secondary slit channels 5 at the outlet and enter the secondary collector channel 15.

[0175] In the case of a hydrogen release reaction, it has proven particularly efficient to feed the hydrogen obtained on the secondary side back to the primary side. Reactor 1 can be designed accordingly, in particular including suitable conduits for such routing.

[0176] During the start-up phase of the process, it is advantageous to first electrically heat the plate heat exchanger 2 to provide heat for the hydrogen release reaction and to initiate it. Heated nitrogen can also be supplied to the primary slotted channels 4 during the start-up phase to preheat the catalyst for the endothermic reaction and thus initiate the reaction.

[0177] Until the hydrogen is available via the hydrogen release reaction, it is expediently supplied to the primary side first. For this purpose, another source can be used temporarily, e.g., an electrolyzer or a separate hydrogen release reaction unit.

[0178] Reference symbol list

[0179] 1 reactor

[0180] 2 plate heat exchangers

[0181] 3 plates

[0182] 4 Primary slot channel

[0183] 5 Secondary slot channel

[0184] 6 Catalyst material

[0185] 7 Primary fluid delivery devices

[0186] 8 Primary distribution channel

[0187] 9 Primary Inlet Pipe

[0188] 10 Secondary fluid delivery devices

[0189] 11 Secondary distribution channel

[0190] 12 Secondary inlet line

[0191] 13 Primary collector channel

[0192] 14 Primary outlet pipe

[0193] 15 Secondary collector channel

[0194] 16 Secondary outlet pipe

[0195] 17 cases

[0196] 18 pressure vessels

[0197] 18a Part

[0198] 18b Part

[0199] 18c flange

[0200] 18d bracket

[0201] 19 Pressure fluid supply devices

[0202] 20 Interior of the pressure vessel

[0203] 21 Pressure fluid circuit

[0204] 22 heat exchangers

[0205] 23 Compressor

[0206] 24 Control device Pressure outlet line Outlet valve Vent valve

Claims

REQUIREMENTS 1. Reactor (1) for carrying out exothermic reactions comprising a plate heat exchanger (2) with a plurality of adjacent plates (3), in particular plates oriented at least substantially parallel to each other, between which gap channels (4, 5) are defined, wherein the gap channels (4, 5) are subdivided into several primary gap channels (4) that are fluidically connected, in particular flow-wise in parallel, and several secondary gap channels (5) that are fluidically connected, in particular flow-wise in parallel, wherein a catalyst material (6) for an exothermic reaction, in particular for a catalytic oxidation reaction, preferably for a catalytic oxidation reaction of hydrogen, and particularly preferably a catalytic combustion of hydrogen with oxygen, is provided in at least one of the primary gap channels (4), preferably in all primary gap channels (4).and wherein primary fluid supply means (7) are provided for supplying a primary fluid to the primary slotted channels (4) and secondary fluid supply means (10) for supplying a secondary fluid to the secondary slotted channels (5), a pressure vessel (18) surrounding the plate heat exchanger (2), pressure fluid supply means (19) configured 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 at least 5 bar, preferably at least 10 bar, and especially preferably at least 20 bar, in the pressure vessel (18).

2. Reactor (1) according to claim 1, characterized in that pressure control means are provided, and the pressure control means are designed and / or configured such that the pressure difference prevailing during operation of the reactor (1) between the pressure in the pressure vessel (18) and the pressure in at least one of the secondary slotted channels (5), preferably in all secondary slotted channels (5), is adjustable, preferably controllable, in particular, wherein the pressure control means are designed and / or configured to maintain 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 slotted channel (5), preferably in all secondary slotted channels (5), and / or to maintain 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 to maintain a pressure at least 100 mbar above or below the pressure in at least one of the secondary slot channels (5), preferably in all secondary slot channels (5).

3. Reactor (1) according to claim 2, characterized in that the pressure control means comprise a pressure measuring device for measuring the pressure in the pressure vessel (18) and / or the pressure in at least one line upstream of the pressure vessel (18) and / or in at least one line downstream of the pressure vessel (18), and a secondary pressure measuring device for measuring the pressure in at least one of the secondary slotted channels (5) and / or the pressure in at least one line upstream of the secondary slotted channels (4) and / or in at least one line downstream of the secondary slotted channels (4), 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 / or the pressure in at least one of the The pressure vessel (18) is located upstream and / or in at least one line downstream of the pressure vessel (18) on the one hand, and the pressure in at least one of the secondary slotted channels (5) and / or the pressure in at least one line upstream and / or in at least one line downstream of the secondary slotted channels (4) on the other hand.

4. Reactor (1) according to one of the preceding claims, characterized in that 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, is provided in at least one of the secondary slit channels (5), preferably in all secondary slit channels (5).

5. Reactor (1) according to one of the preceding claims, characterized in that the plate heat exchanger (2) comprises a preferably electric heating device, in particular wherein one or more plates (3) of the plate heat exchanger (2) are preferably electrically heatable by means of the heating device, and / or that a heating device arranged outside the pressure vessel (18) is provided, by means of which the secondary medium, which can be supplied to the secondary slotted channels (5) by means of the secondary fluid supply means, can be heated.

6. Reactor (1) according to one of the preceding claims, characterized in that the catalyst material provided in the primary slit channels (4) comprises at least one precious 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 in that the primary slit channels (4) and / or the secondary slit channels (5) are provided with stabilizing elements, in particular stabilizing ribs.

8. Reactor (1) according to one of the preceding claims, characterized in 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 inside the pressure vessel (18).

9. Reactor (1) according to one of the preceding claims, characterized in that 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 in that the primary slot channels (4) and the secondary slot channels (5) are not fluidically connected to each other, and / or that the primary slot channels (4) and the secondary slot channels (5) are arranged alternately.

11. Reactor (1) according to one of the preceding claims, characterized in that a pressure fluid circuit (21) is provided, excess pressure fluid is discharged from the pressure vessel (18) and returned to the pressure vessel (18). can be reintroduced, 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 this device before entering the pressure vessel (18) and / or after exiting the pressure vessel (18).

12. Use of a reactor (1) according to any 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 NH3 cracking or methanol reforming or DME reforming or methane steam reforming or LPG reforming or butane or propane dehydrogenation, and / or for heating water to saturated steam or superheated steam.

13. Method for operating a reactor (1) according to any one of claims 1 to 11, comprising the steps - a primary fluid is supplied to at least one primary slit channel (4), preferably to all primary slit 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 slit channel (4), preferably in all primary slit channels (4), - a secondary fluid is supplied to at least one secondary slit channel (5), preferably to all secondary slit channels (5), - a pressure fluid, in particular a pressure gas, is supplied to the pressure vessel (18), preferably wherein the pressure 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 in that the reactor (1) is operated such that the pressure in the pressure vessel (18) 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 slotted channels (5), preferably in all secondary slotted channels (5), and / or that 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 at least one of the secondary slotted channels (5), preferably in all secondary slotted channels (5).

15. Method according to one of claims 13 or 14, characterized in that the pressure fluid is at least partially repeatedly or continuously exchanged, and / or that pressure fluid removed from the pressure vessel (18) is returned to the pressure vessel (18), preferably following cooling and / or heating.

16. Method according to one of claims 13 to 15, characterized in that a primary fluid comprising or being provided as a mixture of hydrogen and oxygen is supplied to the at least one primary slit channel (4), preferably wherein a primary fluid is supplied which is located outside the explosive range, and / or that at least one primary slit channel (4) is supplied with a primary fluid comprising a retentate, in particular from product processing.

17. Method according to one of claims 13 to 16, characterized in that boiling methanol or boiling water or a thermal oil or a molten salt or a gas, in particular compressed air, is supplied as a secondary fluid to the at least one secondary slot channel (5).

18. Method according to one of claims 13 to 17, characterized in that a reaction fluid for an endothermic reaction is supplied to the at least one secondary slit channel (5) as a secondary fluid, and 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 in the at least one secondary slit channel (5).

19. Method according to claim 18, characterized in 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 in that methanol reforming is carried out in the at least one secondary slit channel (5) and that a catalytic oxidation reaction of a part of the product stream is carried out in the at least one primary slit channel (4).

21. Method according to one of claims 13 to 20, characterized in that the secondary fluid is evaporated and / or superheated as a result of absorbing the heat released during the exothermic reaction in the at least one primary slot 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 in that saturated steam or superheated steam is generated in at least one of the secondary slotted channels (5), preferably in all secondary slotted channels (5).

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