WO2025237751A1 - Reactor for carrying out reactions, in particular exothermic reactions, and use and method for operating such a reactor - Google Patents

Abstract

The present invention relates to a reactor (1) for carrying out reactions, 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 primary gap channels (4) and a plurality of secondary gap channels (5), wherein a catalyst material (6) 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

DESCRIPTION

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

The invention relates to a reactor for carrying out, in particular, exothermic reactions. Furthermore, the invention relates to the use of and a method for operating such a reactor.

The applicant is aware that different reactor types are used for exothermic reactions, specifically cooled tube bundle reactors, adiabatic beds with intercooling or cold gas injection, and fluidized bed reactors.

Especially for ammonia (NH3) synthesis, adiabatic beds with combined intercooling and cold gas injection are used. The reaction takes place at high pressures and temperatures either on iron catalysts (350°C to 550°C, 100 to 300 bar) or ruthenium (Ru) catalysts, where somewhat lower temperatures are also possible.

Recently, bimetals containing cobalt and so-called single-atom catalysts have also been proposed as catalysts for ammonia synthesis. The former are discussed, for example, in the publication "Iron-Cobalt-Based Materials: An Efficient Bimetallic Catalyst for Ammonia Synthesis at Low Temperatures" by Rohit K. Rai et al., ACS Catal. 2022, 12, 1, 587–599. Ammonia synthesis using single-atom catalyst beds is the subject of the publication "Ammonia Synthesis Using Single-Atom Catalysts Based on Two-Dimensional Organometallic Metal." Phthalocyanine Monolayers under Ambient Conditions” by Chun-Xiang Huang et al., ACS Appl. Mater. Interfaces 2021, 13, 1, 608 to 621.

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. In adiabatic beds with cold gas injection, the equilibrium position is shifted negatively, and the catalyst beds are also not optimally utilized overall. Cooled tube bundle reactors, while offering comparatively good catalyst utilization, are generally very expensive because their size scales with the number of tubes. Boiling water cooling is not suitable for NH3 synthesis because 350°C is too close to the critical point.

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 524227 B2.

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 in a cell block surrounded by a pressure vessel.

US 6 689 499 B2 yields pressurized fuel cell generator modules protected by purge gas.

JP 3 845 780 B2 discloses atmospheric and pressurized SOFC power generation systems. It is therefore an object of the present invention to provide an alternative reactor for carrying out, in particular, 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.

The first-mentioned problem is solved according to the invention by a reactor for carrying out, in particular, exothermic reactions, comprising a plate heat exchanger with a plurality of adjacent plates, in particular plates oriented at least substantially parallel to one another, between which gap channels are defined, wherein the gap channels are divided into several primary gap channels that are fluidically interconnected, in particular fluidically connected in parallel, and several secondary gap channels that are fluidically interconnected, in particular fluidically connected in parallel, wherein a catalyst material, in particular for ammonia synthesis or methanol synthesis or dimethyl ether synthesis or a hydrogen release reaction, is provided in at least one of the primary gap channels, preferably in all primary gap channels, and wherein primary fluid supply means for supplying a primary fluid to the primary gap channels and secondary fluid supply means for supplying a secondary fluid to the secondary gap channels are provided, and a pressure vessel that surrounds the plate heat exchanger. Pressure fluid supply means designed to supply a pressure fluid to the pressure vessel and, in particular, to maintain an increased pressure of at least 2 bar in the pressure vessel, especially of we- to generate at least 5 bar, preferably at least 10 bar, particularly preferably at least 20 bar.

The second problem is solved 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 slit channel, preferably all primary slit channels, and a particularly exothermic reaction is carried out in the at least one primary slit channel, preferably in all primary slit channels,

- a secondary fluid is supplied to at least one secondary slit channel, preferably to all secondary slit channels,

- a pressure fluid, in particular a pressurized gas, is supplied to the pressure vessel, preferably comprising H2 and/or N2, particularly preferably a mixture of H2 and N2 or a mixture of H2 and CO2 or synthesis gas.

In other words, the present invention proposes the use of a plate heat exchanger for carrying out reactions, such as exothermic reactions, for example, ammonia synthesis. 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, a heat transfer medium flows through the gap channels of both groups. An efficient exchange of thermal energy takes place between the heat transfer media.

According to the invention, at least one group of the slit channels is used to carry out or operate a thermal reaction. These slit channels, preferably those 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, for example, a catalyst material for an exothermic reaction, such as a catalyst material for ammonia synthesis, methanol synthesis, dimethyl ether synthesis (DM E synthesis), or a hydrogen release reaction. A primary fluid is supplied to the primary slit channels for the reaction. This can also be referred to as the reaction fluid.

The other group of slit channels, referred to here as secondary slit channels, can be used, for example, to dissipate heat released during an exothermic reaction. In this configuration, one can also say that the primary slit channels serve 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 acts as a cooling medium.

It should be noted that, although it has proven particularly suitable to provide a catalyst material for an exothermic reaction in the primary slit channels of the reactor according to the invention and to carry out an exothermic reaction, this is by no means mandatory. Rather, it is also possible to provide a catalyst material for an endothermic reaction in the primary slit channels. In that case, the catalyst material is introduced via the secondary slit channels or the material in the During operation, the secondary fluid flowing through the heat exchanger does not dissipate heat released during an exothermic reaction on the primary side. Instead, heat can be supplied via the secondary side for the endothermic reaction on the primary side. In other words, the secondary slotted channels can be used not only as cooling channels but also as heat supply channels, and the secondary fluid can be used accordingly as the heating fluid.

Preferably, a catalyst material for a thermocatalytic reaction is provided in the primary slit channels. The reactor according to the invention is, in particular, a thermocatalytic reactor.

The reactor according to the invention is not an electrolytic reactor. In other words, it is not a reactor in which chemical reactions driven by electricity, in particular redox reactions forced by electrical energy, can take place or do take place.

Accordingly, no electrolytic reactions are carried out in the primary or secondary slit channels within the framework of the method according to the invention.

Advantageously, the primary and secondary slit channels are not fluidically connected.

It has also proven particularly advantageous in the reactor according to the invention if the primary and secondary slit channels are arranged alternately, in other words, if a primary slit channel alternates with a secondary slit channel. This allows, for example, particularly efficient cooling in the case of an exothermic reaction. the primary side or heat input in the case of an endothermic reaction on the primary side.

It should be noted that the secondary slit channels may be free of catalyst material, but this is not necessarily the case. They may, for example, contain such material to utilize cooling via an endothermic reaction on the secondary side, which will be discussed in more detail below. Any catalyst material present in the secondary slit channels, which can also be referred to as "secondary catalyst material" for clarity, may differ from the catalyst material in the primary slit channels.

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. Reactions, for example exothermic reactions, can take place at high pressures and temperatures without the need for complex sealing of the plate heat exchanger or the primary and/or secondary channels. It should be noted that it is also possible for a reactor according to the invention to have more than one plate heat exchanger arranged in the pressure vessel.

The present invention combines several advantages. On the one hand, the reactor according to the invention can be manufactured relatively cost-effectively. It offers good thermal integration, especially compared to adiabatic beds with intercooling. It also offers high load flexibility. Rapid load changes and high responsiveness are possible. This is particularly true since 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 or heating during the start-up phase, which will be discussed in more detail below.

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.

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. 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 the primary gas or a component thereof. If the pressure vessel is filled with primary gas, it is advantageous to monitor for the reaction product. For example, if the reaction to NH3 occurs and N2 is supplied to the pressure vessel as a pressurized gas (in other words, if it is purged with N2), the leakage sensor is advantageously used to test for or monitor for H2.

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

The catalyst material provided in the primary slit channel(s) can, for example, be iron- and/or ruthenium- and/or copper-zinc-based. Alternatively or additionally, it is possible that it comprises or is provided by one or more bimetals, preferably with a cobalt component. It is also possible, again alternatively or additionally, that the catalyst material provided in the primary slit channel(s) comprises or is provided by at least one single-atom catalyst and/or comprises or is provided by at least one SCALMS catalyst.

Single-atom catalysts are also referred to as one-atom catalysts. They preferably comprise or consist of single-atom alloys. SCALMS stands for “Supported Catalytically Active Liquid Metal Solutions”.

The catalyst material provided in the primary slotted channel(s) can also be located on a support material. The catalyst material, or the support material thereof, can be granular, for example. It can be in the form of pellets, or pellets containing the catalyst material can be provided in the primary slotted channels. Alternatively or additionally, the catalyst material can also be in the form of at least one coating, for example, obtained by a washcoat. For example, plates of the plate heat exchanger can be coated with the catalyst material or a coating material containing the catalyst material. One or more insert plates, consisting of the catalyst material or coated with it, for example by a washcoat, can also be arranged in the primary slotted channels, which can simplify manufacturing. 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 slotted channels and/or the secondary slotted channels. If a catalyst material is also provided in the secondary slit channels, in particular one for an endothermic reaction, the above may alternatively or additionally apply to this catalyst material as well.

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 primary slot channels, preferably in all primary slot channels, is adjustable, preferably controllable. In an advantageous further development of the method according to the invention, 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 primary slot channels, preferably in all primary slot 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 primary slot channels, preferably in all primary slot channels. In other words, when setting or controlling a maximum pressure difference between the interior of the pressure vessel and the reaction pressure in one or more primary slot channels, a percentage difference and/or absolute deviations can be used.

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

In other words, the pressure in the pressure vessel is then the same as, or at least very similar to, the reaction pressure in one or more primary slit channels. The pressure of the pressurized gas is expediently adjusted to the reaction pressure during operation. The pressure control devices can be designed and/or configured accordingly.

If pressure control means are present, these can alternatively or additionally be designed and/or configured in such a way that the pressure difference that occurs 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 prevails in at least one of the secondary slot channels, preferably in all secondary slot channels, is adjustable, preferably controllable.

The reactor can further be operated such that the pressure in at least one of the secondary slotted channels, preferably the pressure in all secondary slotted 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 slotted channels, preferably in all primary slotted channels. Alternatively or additionally, the reactor can be operated such that the pressure in at least one of the secondary slotted channels, preferably the pressure in all secondary slotted 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 slotted channels, preferably in all primary slotted channels.

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

In other words, operation can also be carried out in such a way that the secondary slotted channels have the same or a similar pressure as the primary slotted channels, which is particularly possible, for example, when a thermal oil is used as the secondary fluid. For this purpose, the pressure in the secondary slotted channels is expediently adjusted to the pressure in the primary slotted channels, since the reaction pressure depends on the operating conditions.

However, a pressure difference can also exist, and (significantly) different pressures are also possible in principle. The secondary gap channels, or the plates defining the secondary gap channels, can then be particularly affected by... These components may be welded together, or suitable seals and sufficient contact pressure of the plates may be implemented to allow for higher pressure differentials. The same can apply alternatively or additionally to the primary slot channels or the plates defining the primary slot channels.

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.

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

As a rule, the pressure in the primary channel(s) and the pressure in the primary fluid supply to the primary channel(s) and/or in the primary fluid discharge from the primary channel(s) are almost identical. This is particularly true if no valve or similar device is located between the plate heat exchanger or its primary channel(s) and at least one supply or discharge line.

The same applies to the secondary slotted channels and the pressure vessel, and at least one supply and one discharge line in each case. Here, too, the pressure is almost identical, especially if no valve or similar device is arranged between the secondary slotted channels or the pressure vessel and a supply or discharge line.

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 primary slot channels, preferably in all primary slot channels, and/or in at least one line upstream or downstream of the primary slot channels on the other hand, is adjustable, preferably controllable. 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.

Furthermore, at least one primary pressure measuring device can 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.

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, preferably exactly one, line upstream or downstream of the pressure vessel and the pressure in at least one of the primary slotted channels. If a primary differential pressure measuring device is present, it can alternatively or additionally be configured to measure the pressure difference between the pressure in the pressure vessel and the pressure in at least one of the primary slotted channels. 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 primary slotted channels and/or in at least one line downstream of the primary slotted channels on the other.

At least one secondary pressure measuring device can also 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.

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 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 secondary slotted channels on the other. 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 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 secondary slotted channels and/or in at least one line downstream of the secondary slotted channels on the other. The line upstream of the primary slotted channel(s), 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 arms 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.

Similarly, the line downstream of the primary slotted channel(s), 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.

Furthermore, the line upstream of the secondary slotted channels, 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.

The line downstream of the secondary slotted channels, in which the pressure can be measured alternatively or additionally, can be, for example, a secondary outlet line and/or a secondary- This refers to 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 other lines.

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.

The pressure measuring device and/or the primary pressure measuring device and/or the secondary pressure measuring device and/or the primary differential pressure measuring device and/or the secondary differential pressure measuring device can be part of the reactor's pressure control means.

The pressure measuring device and/or the primary pressure measuring device and/or the secondary pressure measuring device and/or the primary differential pressure measuring device and/or the secondary differential pressure measuring device may 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 may be controlled to achieve the desired pressure. The pressure fluid supply means, which may include at least one valve and/or at least one pump and/or at least one compressor, may be connected to the pressure control means, in particular to a control device for these. 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 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 primary slotted channels and/or in at least one, preferably exactly one, line upstream or downstream of the primary 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 line upstream or downstream of the pressure vessel on the one hand and 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 on the other.

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 secondary slotted channels and/or in at least one, preferably exactly one, line upstream or downstream of the secondary slotted channels can be adjusted, in particular regulated, depending on 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. 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 secondary slotted channels and/or in at least one, preferably exactly one, line upstream or downstream of the secondary 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 line is adjustable, in particular controllable, 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 secondary slotted channels and/or in at least one, preferably exactly one, line upstream or downstream of the secondary slotted channels on the other hand.

For example, the control device for the pressure control means can be conveniently connected to the secondary fluid supply means.

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

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, they can each be provided by only one supply line or inlet. The pressurized gas supplied to the pressure vessel can, for example, comprise or consist of H2 and/or N2, preferably a mixture of H2 and N2 or a mixture of H2 and CO2 or synthesis gas or an inert gas or hydrogen (H2) or forming gas, in particular a mixture of nitrogen (N2) and hydrogen (H2).

Another particularly advantageous embodiment is characterized in that the primary fluid supply means comprise or are provided by a primary inlet line, and the pressure fluid supply means comprise or are provided by a pressure inlet line, and the primary inlet line and the pressure inlet line are fluidically connected to each other, so that a primary fluid that can be supplied to the primary slotted channels can also be supplied to the pressure vessel as a pressure fluid. In other words, a feed fluid, in particular feed gas, which is supplied to the primary slotted channels, or a partial flow thereof, can also be used as a pressure fluid, in particular a pressure gas, for the pressure vessel.

The method according to the invention can be characterized analogously in that the primary fluid supplied to the at least one primary slot channel is also supplied to the pressure vessel as pressure fluid, preferably wherein the primary fluid supplied to the at least one primary slot channel and the pressure vessel originates from a common source. The reactor according to the invention can be designed and/or configured accordingly.

The primary fluid supply and pressure fluid supply, or the primary inlet line and the pressure inlet line, can be, for example, fluidically connected or connectable to a common primary fluid source. A primary fluid feed line can also be provided upstream of the primary fluid supply and pressure fluid supply. be, which is fluidically connected to both the primary fluid supply means and the pressure fluid supply means.

It can further be provided that the pressurized fluid and the primary fluid are (re)combined after leaving the pressure vessel. In this case, the amount of pressurized fluid added to the primary fluid is preferably controlled, in particular regulated, for example by at least one controllable or adjustable valve. It is then expediently ensured that the pressurized fluid constitutes only a small fraction of the primary fluid, for example 1 to 10% of the primary fluid.

Another embodiment of the reactor according to the invention is characterized accordingly in that a pressure outlet line is provided through which pressure fluid can exit the pressure vessel and that a primary outlet line is provided through which primary fluid, which has flowed through the primary slotted channels, can exit the plate heat exchanger and in particular leave the pressure vessel, and the pressure outlet line and the primary outlet line are fluidically connected to each other.

In particular, a bypass may be provided through which the primary fluid is supplied to and discharged from the pressure vessel and recombined with primary fluid that has flowed through and exited the primary slotted channels. The pressure inlet line may be designed as a first bypass line, branching off from the primary inlet line and leading to the pressure vessel, and the pressure outlet line may be designed as a second bypass line leading away from the pressure vessel and, in particular, opening into the primary outlet line. Together, these form the bypass through which a portion of the primary fluid is "captured," bypasses the primary slotted channels, and The fluid is routed through the pressure vessel. A bypass has proven particularly suitable. If the pressure fluid withdrawn from the pressure vessel is also mixed with the primary fluid after exiting the primary channels, it can be achieved very simply that the same pressure prevails in the primary channels and the pressure vessel. A bypass requires comparatively little design effort while simultaneously achieving the desired, as closely matched as possible, pressure conditions.

It should be noted that, in a preferred embodiment, the primary fluid is preheated before entering the primary fluid channel(s). Any planned diversion of primary fluid towards the pressure vessel then conveniently occurs before preheating, which can be achieved, for example, by means of a heat exchanger designed for primary fluid preheating. In other words, a portion of the primary fluid is drawn off cold, i.e., in its unpreheated state, and routed through the pressure vessel—particularly via two bypass lines—so that the pressure vessel can be cooled by the primary fluid, or is cooled during operation.

In an advantageous embodiment, the pressurized fluid can be cooled. The reactor according to the invention can accordingly include a pressurized fluid cooling device for cooling the pressurized fluid. It can be provided that the pressurized fluid is cooled before entering the pressure vessel and/or after exiting the pressure vessel. The pressurized fluid cooling device, if present, can be designed and arranged accordingly.

As mentioned, the discharge fluid from the pressure vessel can also be mixed with the discharge fluid from the primary slit channels, i.e., the reaction discharge fluid. They are mixed. This makes cooling the printing envelope possible without additional large equipment.

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.

The reactor according to the invention can comprise a pressure fluid circuit, in which excess pressure fluid can be removed from the pressure vessel and returned to the pressure vessel.

Within the scope of the present invention, various possibilities exist for cooling in the primary slotted channel(s) in the case of an exothermic reaction. For example, at least one, preferably all, secondary slotted channels can be supplied with a secondary fluid, in particular boiling methanol, or in particular boiling water, or thermal oil, or a molten salt. The plate heat exchanger of the reactor according to the invention, in particular its secondary slotted channels, can be further developed accordingly, for example, by being made of a suitable material.

A suitable coolant as a secondary fluid 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 300°C, which corresponds to a boiling pressure of approximately 3 to 150 bar. A thermal oil is particularly suitable for a comparatively high temperature range of 250°C to 450°C. The same applies to a molten salt, which is especially suitable for... especially for a temperature range of 400°C to 650°C.

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, 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, specifically one for an endothermic reaction, is also supplied to the at least one secondary slit channel, and that an endothermic reaction, in particular a hydrogen release reaction, is carried out in the at least one secondary slit channel. A hydrogen-rich compound can then be supplied as a secondary fluid to the at least one secondary slit channel, preferably to all secondary slit channels.

In particular, if an exothermic ammonia synthesis is carried out on the primary side, hydrogen released on the secondary side via a hydrogen release reaction can then be used for ammonia synthesis, in other words, fed back to the primary side of the plate heat exchanger. This has proven to be particularly efficient.

During a start-up phase to initiate the process, it is then expedient to first heat the plate heat exchanger, preferably electrically. metauschers to provide heat for the endothermic reaction and to initiate it, in particular a hydrogen release reaction.

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 slotted channels during a start-up phase.

It is also possible to supply a heated fluid or gas, e.g., heated nitrogen, 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.

Alternatively or additionally, the secondary side can be used to preheat 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 warming the secondary fluid. This eliminates the need for electric heating plates in the reactor.

If no hydrogen is initially available via dehydrogenation during the start-up phase, it can be supplied to the primary side first. Accordingly, during a start-up phase, hydrogen can be supplied to at least one, preferably all, of the primary slit channels from a other sources, in particular hydrogen, which is provided by means of an electrolyzer or a separate hydrogen release reaction facility.

Once the hydrogen release reaction has started, hydrogen from this reaction can be added to the nitrogen loop. The start-up phase is then complete, the external heating can be switched off, and the supply of hydrogen from another source can be stopped.

As mentioned, one of the exothermic reactions that can be used within the scope of the present invention is the ammonia synthesis. Regarding this, the following applies:

N ₂ (g) + 2H ₂ (g) 2NH ₃ (g) AH° = -91.88 kJ moM

This is a strongly exothermic equilibrium reaction that proceeds at high pressures up to 300 bar. Conventionally, an iron catalyst is used, which requires operating temperatures above 300°C and below 520°C. Therefore, cooling with water is rather impractical (too close to or above the critical point). Therefore, particularly in the case of ammonia synthesis within the scope of the present invention, a thermal oil or even a variant of the endothermic reaction, especially a hydrogen release reaction, is preferably used on the secondary side of the plate heat exchanger.

Another advantageous embodiment of the invention is characterized in that the secondary fluid evaporates and/or superheats 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 supplied 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. The reactor according to the invention can accordingly comprise at least one solid oxide electrolyzer cell.

Furthermore, it may be provided that at least one of the secondary slot channels is subdivided into several partial secondary slot channels, preferably connected in parallel to each other in terms of flow characteristics. Such a subdivision, so to speak into several "sub-secondary slot channels", can also be provided for all secondary slot channels.

Alternatively or additionally, at least one, or even all, of the secondary slit canals may exhibit a meandering course. If there is a subdivision into several "sub-secondary slit canals," these may also be meandering.

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

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.

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, with each aligned hole forming a transverse channel through the plates and the gap channels defined between them. extending, in particular cylindrical, primary-secondary distribution or collector 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.

The holes are preferably located in the edge area of the plates. If the plates are rectangular, especially if they are at least substantially rectangular or square, one of the holes can be found, for example, in or near each corner of each plate.

Another 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, in particular a central one, and a primary outlet line, in particular a central one. Similarly, the secondary slotted channels can be connected to a secondary inlet line, in particular a central one, and a secondary outlet line, in particular a central one.

The primary slit channels can be connected, for example, to a primary inlet line via a primary distributor channel and to a primary outlet line via a primary collector channel. Similarly, the secondary slit channels can be connected to a secondary inlet line via a secondary distributor channel and to a secondary outlet line via a secondary collector channel.

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... The plates are structurally identical. They are preferably made of metal or comprise metal.

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.

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

The plate heat exchanger may also include a housing. In this case, the housing may in particular have an insulating layer made of a thermally insulating material.

Within the scope of the present invention, various types of exothermic reactions can in principle be carried out or used.

It has proven particularly suitable if the exothermic reaction takes place in at least one primary slit channel, preferably in all primary slit channels,

- oxygen removal from a hydrogen stream, in particular a hydrogen stream originating from electrolysis (especially PEM, AEL, AEM), preferably at temperatures T = 70 to 100°C, and pressures p to 40 bar, or

- hydrogen removal from an oxygen stream, especially one from electrolysis (especially PEM, AEL, AEM) stam- oxygen flow, preferably at temperatures T = 70 to 150°C, and pressures p up to 40 bar, or

- a methanol synthesis, preferably from CO2 or synthesis gas and/or with copper-zinc-based catalysts for methanol formation and/or at temperatures T = 200 to 300°C, and pressures p up to 80 bar, or

- a DME synthesis, preferably from CO2 or synthesis gas and/or with copper-zinc-based catalysts for methanol formation and/or at temperatures T = 200 to 300°C, and pressures p up to 80 bar, or

- an ammonia synthesis, preferably at temperatures T = 300°C to 520°C and pressures p up to 300 bar, or

- SNG production, in particular from carbon dioxide (CO2) or synthesis gas, is carried out, preferably at temperatures T = 250 to 400°C and pressures p up to 80 bar. SNG stands for Synthetic Natural Gas.

PEM electrolysis stands for "Proton Exchange Membrane" electrolysis. AEL electrolysis stands for alkaline electrolysis. AEM electrolysis stands for "Anion Exchange Membrane" electrolysis.

The invention also relates to the use of a reactor according to the invention for ammonia synthesis or methanol synthesis, in particular from carbon dioxide (CO2) or synthesis gas, or dimethyl ether synthesis, in particular from carbon dioxide (CO2) or synthesis gas, or for oxygen removal from a hydrogen stream, in particular from electrolysis, or for hydrogen removal from an oxygen stream, in particular from electrolysis. for the production of Synthetic Natural Gas from carbon dioxide (CO2) or synthesis gas.

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. The drawing shows:

Figure 1 shows a first embodiment of a reactor according to the invention in a purely schematic sectional view.

Figure 2 is a perspective exterior view of the reactor from Figure 1.

Figure 3 shows another purely schematic sectional view of the reactor from Figure 1, and

Figure 4 shows a second embodiment of a reactor according to the invention in a purely schematic sectional view.

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

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.

Reactor 1 is designed to carry out exothermic reactions.

Reactor 1 comprises a plate heat exchanger 2 with a plurality of adjacent, in particular at least substantially parallel to each other. oriented, plates 3. Of the plates 3, only a few are shown in Figure 1, designated with the reference numeral 3. 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.

Between the plates 3, gap channels 4, 5 are defined; specifically, one gap channel 4, 5 is located 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, fluidically connected in parallel), and several secondary gap channels 5, which are fluidically interconnected (specifically, fluidly 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 slit channel 4 is therefore 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 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.

Each of the primary slit 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 primary slit channels 4. In Figure 1, a granular catalyst material 6 is schematically indicated by way of example, and even then only over a section of the respective primary slit channel 4. It is understood that the primary slit channels 4 can be filled with, for example, a granular catalyst material 6 along their entire length. Alternatively, it is also possible Alternatively, the plates 3 may be coated with catalyst material 6 or a coating material containing catalyst material 6. One or more insert plates, made of or coated with the catalyst material (e.g., by a washcoat), may also be arranged in the primary slot channels 4, which can simplify manufacturing. The catalyst material may also be present in the form of catalytically active structures. For example, catalytically active networks may be provided in the primary slot channels and/or the secondary slot channels.

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 visible in Figure 1, but is not shown again in Figure 2.

The present case concerns a catalyst material 6 for ammonia synthesis, for which the embodiment of a reactor 1 according to the invention shown in Figure 1 is used.

Regarding ammonia synthesis, the following applies:

N ₂ (g) + 2H ₂ (g) 2NH ₃ (g) AH° = -91.88 kJ mol- ¹

This is a highly exothermic equilibrium reaction that occurs at high pressures up to 300 bar.

The catalyst material 6 for ammonia synthesis can, for example, be an iron-based or a ruthenium-based catalyst material 6. The catalyst material 6 can also comprise one or more bimetals, preferably with a cobalt component, or be provided by It may also include or be provided by at least one so-called single-atom catalyst and/or at least one so-called SCALMS catalyst for ammonia synthesis.

In the illustrated embodiment, an iron-based catalyst material is provided in the primary slot channels 4, and the same catalyst material 6 is used in all primary slot channels 4. Iron catalysts generally require operating temperatures in the range of 300°C to 520°C.

It should be noted that alternative exothermic reactions to ammonia synthesis, which can be carried out in a reactor 1 according to the invention, or in other words, for which a reactor 1 according to the invention can be used, include, for example, methanol synthesis, DME synthesis, or oxygen removal from a hydrogen stream, particularly from electrolysis, or hydrogen removal from an oxygen stream, particularly from electrolysis, or SNG production, particularly from carbon dioxide (CO2) or synthesis gas. Appropriate catalyst materials suitable for the respective exothermic reaction are then provided in the primary slit channels 4.

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 forming gas, specifically a mixture of nitrogen (N2) and hydrogen (H2). The primary fluid can also be referred to as the reaction fluid or, in this case, the reaction gas. The primary fluid supply means 7 comprise at least one compressor and at least one valve, which are not shown separately in the purely schematic Figure 1. As can be seen in Figure 1, the primary slot 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 slot channels 4 via the primary distribution channel 8.

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 at least one valve, which are not shown separately in the purely schematic figure 1.

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.

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 can be collected and can exit the plate heat exchanger 2 via a central primary outlet line 14.

On the output side of the secondary slit channels 5, a secondary collector channel 15 is provided in an analogous manner, in which all secondary- Fluid exiting from the 5 slit channels can be collected and can exit the plate heat exchanger 2 via a central secondary outlet line 16.

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

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.

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, with each aligned hole forming a primary or secondary distribution or collector channel 8, 11, 13, 15, extending transversely through the plates 3 and the defined gap channels 4, 5, and being cylindrical in shape. This is known from conventional or conventionally used plate heat exchangers. The connection of the respective distribution or collector channel 8, 11, 13, 15 with the associated slot channels, or the separation thereof, can then be realized 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, as in the illustrated- In the example shown, which is rectangular, one of the holes can be located in or near each corner.

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.

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 in the primary slotted channels 4 during the exothermic reaction, in this case ammonia synthesis. If this is the case, it is advantageous to provide a catalyst material for an endothermic reaction, e.g., a hydrogen release reaction, 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.

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. The hydrogen released as a result of the hydrogen release reaction can then be used for ammonia (NH3) synthesis on the primary side of the plate heat exchanger 2. If an endothermic reaction is used on the secondary side, the plate heat exchanger 2 can be electrically heated to provide heat for the endothermic reaction during a start-up phase. It is also possible for the secondary fluid to be heated externally.

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.

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 bracket 18d, which is preferably attached to the flanges 18c, at a distance from the pressure vessel wall (see Figure 3). It should be noted that the two-part design of the pressure vessel 18 is not recognizable in the purely schematic, simplified figure 1. 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 at least one valve, which are not shown separately in schematic Figure 1.

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 to the outside (to the interior of the pressure vessel 18) during operation when ammonia synthesis is carried out and can therefore be designed more simply with regard to its seals.

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.

For example, an inert gas or hydrogen (H2) or forming gas, in particular a mixture of nitrogen (N2) and hydrogen (H2), can be supplied to the pressure vessel 18 as a pressurized pressurized gas by means of the pressurized fluid supply means 19.

It is also possible, and has proven particularly suitable, if the feed gas supplied to the primary slit channels 4 for the exothermic reaction is simultaneously used as a pressurized gas for the pressure vessel 18. Cooling of the pressurized fluid can be provided. The reactor 1 shown in Figure 1 comprises a pressurized fluid circuit 21 with a pressurized fluid cooling device, which includes or is provided by a heat exchanger 22. Pressurized gas can be drawn from the pressure vessel 18 via the pressurized fluid circuit 21, cooled by means of the pressurized fluid cooling device, in particular by means of the heat exchanger 22, and then reintroduced into the pressure vessel 18. The circuit 21 also includes a compressor 23. Additional cooling can be achieved via a recirculated, cooled pressurized gas.

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

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 primary gap channels 4 can be adjusted, preferably controlled.

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 primary gap channels 4. For this purpose, the control device 24 is expediently connected to the primary fluid supply means 7 and the pressure fluid supply means 19, for example, compressors thereof.

Pressure measuring devices, such as pressure sensors, may be provided for the metrological measurement of the pressure in the pressure vessel 18 and/or the pressure in at least one primary slot channel 4. Alternatively or additionally, Additionally, a primary 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 primary slot channels 4. Alternatively or additionally, a pressure measuring device can be provided for measuring the pressure in at least one secondary slot channel 5. The pressure measuring devices and/or the primary differential pressure measuring device can be part of the pressure control system. The control unit 24 can 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.

It should be noted that, alternatively or additionally to pressure measurement in the pressure vessel 18 or at least one primary slotted channel 4 or secondary slotted channel 5, the pressure can also be measured in the supply line, specifically in at least one fluid line upstream of the pressure vessel 18 or in at least one line upstream of one or more, possibly even all, primary slotted channels 4 or secondary slotted 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 primary inlet line 9 and/or the primary distribution channel 8, for instance, in at least one of its several arms.

Regarding the secondary slotted channels 5, 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 secondary inlet line 12 and/or the secondary distribution channel 11, for example, in at least one of its several arms. Even with differential pressure measurement, the supply, specifically at least one The line upstream of the pressure vessel 18 or at least one primary slotted channel 4 or secondary slotted channel 5 is shut off.

Alternatively or additionally, pressure measurement can be performed in a feeder line, or in at least one downstream line. 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 primary collector channel 13, for instance, in at least one of its multiple arms. Differential pressure measurement can also be performed in the downstream line, specifically at least one line downstream of the pressure vessel 18 or at least one primary slotted channel 4.

The same applies to the secondary slotted channels 5. At least one pressure measuring device, e.g., at least one pressure sensor, can be provided for measuring the pressure in the secondary outlet line 16 and/or the secondary collector channel 15, for example, in at least one of its several arms. Differential pressure measurement can also be performed on the downstream line, specifically at least one line connected to at least one primary slotted channel 4 or secondary slotted channel 5.

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

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 may also be provided, which activates in the event of excessive pressure (in the (Figure not shown). Pressurized fluid can then pass through such a safety valve to, for example, a flare or safe location.

Furthermore, a vent valve 27 is provided for the plate heat exchanger 2.

During operation of reactor 1, the feed gas is supplied as the primary fluid to the primary slotted channels 4, in other words, the primary side of the plate heat exchanger 2, and a thermal oil is supplied to the secondary slotted channels 5, i.e., the secondary side. Simultaneously, a pressurized gas is supplied to the pressure vessel, in this case also the feed gas, for example from the same source as the feed gas for the primary slotted channels 4.

It should be noted that the primary fluid can be preheated before entering the primary slot channels 4. Reactor 1 may include a heat exchanger for primary fluid preheating (not shown).

In the primary slotted channels 4, ammonia synthesis takes place according to the equation above, releasing heat. Cooling occurs via the secondary side of the plate heat exchanger 2, through the thermal oil flowing through the secondary slotted channels 5.

In the embodiment shown in Figure 1, additional cooling is achieved via the cooled pressure fluid.

The pressure prevailing in the pressure vessel 18 and optionally also in the secondary slotted channels 5 is adjusted to the pressure in the primary slotted channels 4 by means of the control device 24, since the primary pressure depends on the operating state. Specifically, reactor 1 is operated in such a way that the pressure in the pressure vessel 18 is adjusted by means of 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 primary slotted channels.

4. 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 a maximum of 1 bar, preferably a maximum of 100 mbar above or below the pressure in the primary slotted channels 4. The control device 24 is designed and/or configured accordingly.

The reactor 1 is preferably operated such that the pressure in the secondary slotted channels 5 is at most 20%, in particular at most 10%, preferably at most 5%, and most preferably at most 1% above or below the pressure in the primary slotted channels 4. Specifically, the reactor 1 is operated such that the pressure in the secondary slotted channels

5 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 the primary slot channels 4.

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

However, especially if a plate heat exchanger 2 with a more complex seal is used, operation with significantly different pressures is also possible in principle.

The leakage sensor of pressure vessel 18 monitors for a lack of gas. In particular, the leakage sensor detects a leak between primary gap channels 4 and pressure vessel 18 if the pressure in the primary gap channel 4 is slightly higher than in the pressure vessel 18. Ammonia exiting from the primary slotted channels 4 on the outlet side is collected in the primary collector channel 13 and can be routed out of the plate heat exchanger 2 and the pressure vessel 18 via the primary outlet line 14 and put to a desired use.

Heated thermal oil exits from the secondary slotted channels 5 on the outlet side. This heated thermal oil can then be applied to a desired application.

It has proven particularly effective to use the heated thermal oil for steam generation and feed the resulting steam into a solid oxide electrolyzer cell (SOEC) to produce hydrogen. The hydrogen produced in this way can then be used to generate ammonia. Such a system has proven to be especially efficient.

If, as an alternative to a thermal oil, a hydrogen release reaction is used on the secondary side, a hydrogen-rich compound is supplied to the secondary slit channels 5 as a secondary fluid. In the secondary slit channels 5, which in this case are equipped with a suitable catalyst material, hydrogen is released, and hydrogen and a hydrogen-poor compound exit the secondary slit channels 5 at the outlet side and enter the secondary collector channel 15.

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

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.

Once the hydrogen release reaction has started, hydrogen from this reaction can be added to the nitrogen loop, thereby initiating the NH₃ formation reaction in the primary slit channels 4. The start-up phase is then complete, and the external heating can be switched off and the supply of hydrogen from another source can be stopped.

As mentioned above, it has proven particularly suitable if the feed gas supplied to the primary slit channels 4 for the exothermic reaction is simultaneously used as the pressurized gas for the pressure vessel 18. For this purpose, the pressurized fluid feeders 19 can, for example, be fluidically connected to the primary fluid feeders 7 and supply feed gas from a common source.

In particular, a bypass may be provided through which a portion of the primary fluid is "tapped off" before entering the primary slot channels 4, fed to the pressure vessel 18, routed out of it again, and mixed with the primary fluid that has flowed through the primary slot channels, i.e., with the The primary fluid is recombined after the reaction. In the second embodiment of a reactor 1 according to the invention, shown in Figure 4, such a bypass is provided. Since the second embodiment largely corresponds to the first embodiment shown in Figure 1, only the few differences will be discussed below.

In the second embodiment, the pressure inlet line is provided by a first bypass line 28, which is fluidically connected to the primary inlet line 9, specifically branching off from it.

As can be seen in Figure 4, the first bypass line 28 connects the primary inlet line 9, through which the primary fluid is also supplied to the primary slotted channels 4, to the interior of the pressure vessel 18. The end 29 of the bypass line 28, which opens into the pressure vessel 18, thus forms an inlet for the primary fluid, which is also used here as the pressure fluid, into the pressure vessel 18. In this embodiment, the pressure fluid supply means can be provided solely by the bypass line 28. In particular, a separate compressor used only for the pressure fluid is not required.

After leaving the pressure vessel 18, the pressurized fluid (here also primary fluid) is recombined with the primary fluid exiting the primary slot channels 4. The pressurized outlet line is designed as a second bypass line 30, which fluidically connects the interior 20 of the pressure vessel 18 to the primary outlet line 14, specifically leading into the primary outlet line 14 (see Figure 4). A valve 31 is provided in the second bypass line 30. Alternatively or additionally, a valve can also be provided in the first bypass line 28 (not shown). The two bypass lines 28, 30 represent a particularly simple design for achieving consistent pressure conditions in the pressure vessel 18 and the primary slotted channels 4. Since the primary fluid bypasses into and through the pressure vessel 18 via the two bypass lines 28, 30, the pressure in the primary fluid channels 4 and the pressure in the interior of the pressure vessel 18 automatically match. Control or regulation based on measured pressure or differential pressure values is not required. However, it is of course possible that pressure monitoring and active pressure control or regulation may be implemented (additionally). Accordingly, the second embodiment can, for example, include a primary differential pressure measuring device in addition to the two bypass lines 28, 30 for measuring the pressure difference between the pressure in the pressure vessel 18 and the pressure in the primary slotted channels 4.

The valve 31 provided in the pressure outlet line formed by the second bypass line 30 can be connected to a control unit 24 of the reactor 1, via which its valve position can be adjusted. The valve position, in particular, determines how much of the primary fluid is routed through the pressure vessel 18 via the bypass 28, 30. This also determines the degree to which the pressure vessel 18 is cooled by the primary fluid. A portion of the primary fluid intended for the pressure vessel 18 is advantageously "diverted" before preheating. Primary fluid preheating before entering the primary slotted channels 4 can, for example, take place in a heat exchanger provided for this purpose, which is then advantageously located downstream of the branch point of the bypass line 28 from the primary inlet line 9 and upstream of the pressure vessel 18 or plate heat exchanger 2, in the direction of primary fluid flow. Figure 4 shows such a heat defrost The primary fluid preheating circuit is not shown for the sake of clarity. Similarly, a control unit 24, which may also be present in the second embodiment, is not shown again in Figure 4, but is only visible in Figure 1.

Since, in the second embodiment according to Figure 4, the pressure vessel 28 can be cooled via the "bypass primary fluid", no additional pressure fluid circuit 21 with heat exchanger 22 is required, as can be seen in the first embodiment from Figure 1. However, it is also possible that such a circuit is additionally provided in the example from Figure 4 (not shown).

Reference symbol list

1 reactor

2 plate heat exchangers

3 plates

4 Primary slot channel

5 Secondary slot channel

6 Catalyst material

7 Primary fluid delivery devices

8 Primary distribution channel

9 Primary Inlet Pipe

10 Secondary fluid delivery devices

11 Secondary distribution channel

12 Secondary inlet line

13 Primary collector channel

14 Primary outlet pipe

15 Secondary collector channel

16 Secondary outlet pipe

17 cases

18 pressure vessels

18a Part

18b Part

18c flange

18d bracket

19 Pressure fluid supply devices

20 Interior of the pressure vessel

21 Pressure fluid circuit

22 heat exchangers

23 Compressor

24 Control unit 25 Pressure outlet line

26 Exhaust valve

27 Vent valve

28 First bypass line 29 Pressure fluid inlet

30 second bypass line

31 Valve

Claims

REQUIREMENTS 1. Reactor (1) for carrying out reactions, in particular exothermic reactions, comprising a plate heat exchanger (2) with a plurality of adjacent plates (3), in particular plates oriented at least substantially parallel to one another, between which gap channels (4, 5) are defined, wherein the gap channels (4, 5) are divided 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), in particular for ammonia synthesis or methanol synthesis or dimethyl ether synthesis or a hydrogen release reaction, 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 gap channels (4) and secondary fluid supply means (10) are provided for supplying a Secondary fluids are provided for the secondary slot channels (5), a pressure vessel (18) surrounding the plate heat exchanger (2), pressure fluid supply means (19) 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 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 primary slotted channels (4), preferably in all primary slotted channels (4), 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%, more particularly 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 of the primary slotted channels (4), preferably in all primary slotted channels (4), and/or to maintain the pressure in the pressure vessel (18) during operation of the reactor (1) by a maximum of 5 bar, more particularly by a maximum of 1 bar, preferably by a maximum of 100 mbar above or below the pressure to be retained in at least one of the primary slit channels (4), preferably in all primary slit channels (4). 3. Reactor (1) according to claim 2, characterized in that 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 at least one of the primary slotted channels (4), preferably in all primary slotted channels (4) 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 reduce the pressure in at least one of the secondary slotted channels (5), preferably in all secondary slotted channels (5), by a maximum of 20%, more preferably by a maximum of 10%, more preferably by a maximum of 5%, more preferably by a maximum of 1% above or below the pressure in the primary slotted channels (4) during operation of the reactor (1). to maintain the pressure in at least one of the primary slit channels (4), preferably in all primary slit channels (4), and/or to maintain the pressure in at least one of the secondary slit channels (5), preferably in all secondary slit channels (5), 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 primary slit channels (4), preferably in all primary slit channels (4), during operation of the reactor (1). 4. Reactor (1) according to one of claims 2 or 3, 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 primary pressure measuring device for measuring the pressure in at least one of the primary slotted channels (4) and/or the pressure in at least one line upstream of the primary slotted channels (4) and/or in at least one line downstream of the primary slotted channels (4), and/or that the pressure control means comprise a primary 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 line upstream of the pressure vessel (18) 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 primary slotted channels on the other. (4) and/or the pressure in at least one line upstream of the primary slot channels (4) and/or in at least one line downstream of the primary slot channels (4), on the other hand, include. 5. Reactor (1) according to one of the preceding claims, characterized in that the primary fluid supply means (7) comprises a primary inlet line (9) comprise or are provided by, and the pressure fluid supply means (19) comprise or are provided by a pressure inlet line (28) and the primary inlet line (9) and the pressure inlet line (28) are fluidically connected to each other, so that a primary fluid that can be supplied to the primary slot channels (4) can also be supplied to the pressure vessel (18) as a pressure fluid, preferably, wherein the primary inlet line (9) and the pressure inlet line (28) are fluidically connected or connectable to a common primary fluid source. 6. Reactor (1) according to one of the preceding claims, characterized in that a pressure outlet line (30) is provided through which pressure fluid can exit the pressure vessel (18) and that a primary outlet line (14) is provided through which primary fluid, which has flowed through the primary slotted channels (4), can exit the plate heat exchanger (2) and in particular leave the pressure vessel (18), and the pressure outlet line (30) and the primary outlet line (14) are fluidically connected to each other. 7. Reactor (1) according to claims 5 and 6, characterized in that the pressure inlet line is designed as a first bypass line, in particular branching off from the primary inlet line (7) and leading to the pressure vessel (18), and the pressure outlet line (30) is designed by a second bypass line leading away from the pressure vessel and in particular opening into the primary outlet line (14). 8. 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, is provided in at least one of the secondary slit channels (5), preferably in all secondary slit channels (5). 9. 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. 10. Reactor (1) according to one of the preceding claims, characterized in that the catalyst material provided in the primary slit channels (4) is iron and/or ruthenium and/or copper-zinc based, and/or comprises or is provided by one or more bimetals, preferably with a cobalt component, and/or comprises or is provided by at least one single-atom catalyst, and/or comprises or is provided by at least one SCALMS catalyst. 11. 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). 12. Reactor (1) according to one of the preceding claims, characterized in that the plate heat exchanger (2) is provided on its outer side 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 essentially- are rectangular in shape and/or have a profile on at least one side. 13. 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. 14. 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. 15. Reactor (1) according to one of the preceding claims, characterized in that a pressure fluid circuit (21) is provided, through which pressure fluid can be discharged from the pressure vessel (18) and returned to the pressure vessel (18), and/or that a pressure fluid cooling device is provided for cooling the pressure fluid, preferably wherein the pressure fluid cooling device is designed and arranged such that pressure fluid can be cooled by means of it before entering the pressure vessel (18) and/or after exiting the pressure vessel (18). 16. Use of a reactor (1) according to any one of the preceding claims for ammonia synthesis or methanol synthesis, in particular from carbon dioxide or synthesis gas, or dimethyl ether synthesis, in particular from carbon dioxide or synthesis gas, or for oxygen removal from a hydrogen stream, in particular from electrolysis, or for hydrogen removal from a especially oxygen stream originating from electrolysis or for a hydrogen release reaction or for obtaining synthetic natural gas from carbon dioxide or synthesis gas. 17. Method for operating a reactor (1) according to any one of claims 1 to 15, comprising the steps - at least one primary slit channel (4), preferably all primary slit channels (4), is supplied with a primary fluid and a particularly exothermic reaction 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 pressurized gas, is supplied to the pressure vessel (18), preferably comprising H2 and/or N2, particularly preferably a mixture of H2 and N2 or a mixture of H2 and CO2 or synthesis gas. 18. Method according to claim 17, 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 primary slotted channels (5), preferably in all primary 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 primary slotted channels (5), preferably in all primary slotted channels (5). 19. Method according to claim 17 or 18, characterized in that the reactor (1) is operated such that the pressure in at least one of the secondary slotted channels (5), preferably the pressure in all secondary slotted channels (5), 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 slotted channels (4), preferably in all primary slotted channels (4), and/or that the reactor (1) is operated such that the pressure in at least one of the secondary slotted channels (5), preferably the pressure in all secondary slotted channels (5), 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 slotted channels (4), preferably in all primary slotted channels (4). 20. Method according to one of claims 17 to 19, characterized in that the primary fluid supplied to the at least one primary slot channel (4) is also supplied to the pressure vessel (18) as pressure fluid, preferably wherein the primary fluid originating from a common source is supplied to the at least one primary slot channel (4) and the pressure vessel (18), and/or wherein the pressure fluid and the primary fluid are combined after leaving the pressure vessel (18), preferably wherein the amount of pressure fluid supplied to the primary fluid is controlled, in particular regulated, preferably via at least one valve. 21. Method according to one of claims 17 to 20, 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. 22. Method according to one of claims 17 to 21, characterized in that boiling methanol or boiling water or a thermal oil or a molten salt is supplied as a secondary fluid to the at least one secondary slot channel (5). 23. A method according to any one of claims 17 to 22, characterized in that a reaction fluid for an exothermic reaction is supplied to the at least one primary slit channel (4) as the primary fluid and an exothermic reaction is carried out in the at least one primary slit channel (4), preferably in all primary slit channels (4), in particular, wherein a reaction fluid for an endothermic reaction is supplied to the at least one secondary slit channel (5) as the secondary fluid, and an endothermic reaction, in particular a hydrogen release reaction, is carried out in the at least one secondary slit channel (5), preferably, wherein hydrogen released as a result of the hydrogen release reaction is used for ammonia synthesis in the primary slit channels (4). 24. Method according to claim 23, characterized in that in a start-up phase the plate heat exchanger (2) is heated to provide heat for the endothermic reaction, and/or that in a start-up phase at least one of the primary slit channels (4) is supplied with hydrogen from another source, in particular hydrogen supplied by means of an electrolyzer or a separate hydrogen release reaction device. 25. Method according to one of claims 23 or 24, 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 slit channel (4), or that heated secondary fluid is used to generate and/or superheat Steam is used, in particular wherein the generated and/or superheated steam is fed to at least one solid oxide electrolyzer cell to produce hydrogen, preferably wherein the produced hydrogen is used to produce NH3. 26. A method according to any one of claims 23 to 25, characterized in that the exothermic reaction in the at least one primary slit channel (4), preferably in all primary slit channels (4), is carried out as oxygen removal from a hydrogen stream, in particular a hydrogen stream originating from electrolysis, or hydrogen removal from an oxygen stream, in particular an oxygen stream originating from electrolysis, or methanol synthesis, or DME synthesis, or ammonia synthesis, or SNG production, in particular from carbon dioxide or synthesis gas. ```