WO2025237749A1 - Apparatus for heat transfer, use, system and method - Google Patents

Abstract

The present invention relates to an apparatus (V) for heat transfer, comprising: a plate heat exchanger (2) having a plurality of adjacent plates (3) between which gap channels (4, 5) are defined, said gap channels (4, 5) being divided into a plurality of fluidically interconnected primary gap channels (4) and a plurality of fluidically interconnected secondary gap channels (5), wherein 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

Heat transfer device, use, installation and method

The invention relates to a heat transfer device and its use. Furthermore, the invention relates to a system comprising a reactor for a high-temperature process, in particular a cracking process, a reforming process, or a dehydration process. The invention also relates to a method for operating such a system.

High-temperature processes, such as cracking, reforming, or dehydration, typically utilize systems that include a reactor in which the respective high-temperature process can take place. The reactor can be, for example, a fired reactor with a burner, an electrically heated reactor, or an autothermal reactor. Combinations of different heating methods can also be incorporated into or integrated within a single reactor.

The applicant is aware that process-side discharge gases from a high-temperature process (not the exhaust gases from a burner), such as the steam reforming of natural gas, are typically cooled by steam generation. The demands placed on the steam generators used for this purpose are high. In particular, the steam generators are subject to stringent material, pressure, and temperature requirements.

The applicant is further aware that, for example, in steam reforming, the gas exiting the reactor, specifically the steam reformer, which can have a temperature in the range of 750°C to 950°C, is cooled to a temperature level of approximately 400°C, thereby Back reactions must be kept to a minimum, and material problems such as metal dusting must be controlled. The process gas has a pressure of up to 30 bar and must be cooled rapidly to prevent metal dusting and back reactions. However, this rapid cooling, which generates steam, leads to a higher burner output on the reactor's combustion side, since the reaction fluid fed into the reactor (also called the "feed") cannot usually be heated to such a high temperature. This becomes particularly relevant when an autothermal or electrically heated reformer is used instead of a fired steam reformer, as there is no burner flue gas to preheat the reaction fluid before it enters the reactor.

However, there is a need to achieve the most energy-efficient operation possible of plants with reactors for high-temperature processes.

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.

The JP 3 845 780 B2 discloses atmospheric and pressurized SOFC power generation systems. It is therefore an object of the present invention to provide a device of the type mentioned above, the use of which enables the most energy-efficient operation possible of plants for high-temperature processes. Furthermore, it is an object of the present invention to provide a plant of the type mentioned above that can be operated in a particularly energy-efficient manner.

The first-mentioned problem is solved by a heat transfer device comprising a plate heat exchanger with a plurality of adjacent plates, in particular plates oriented at least substantially parallel to each other, between which gap channels are defined, wherein the gap channels are divided into several primary gap channels that are fluidically interconnected, in particular fluidically connected in parallel, and several secondary gap channels that are fluidically interconnected, in particular fluidically connected in parallel, wherein primary fluid supply means are provided 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, 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 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.

The second task is solved by a system comprising a reactor for a high-temperature process, in particular a cracking process. a process or a reforming process or a dehydration process, and a device according to the invention, wherein the primary slotted channels are fluidically connected to an inlet of the reactor and wherein an outlet of the reactor is fluidly connected to the secondary slotted channels, so that a reaction fluid to be supplied to the reactor can be supplied to the primary slotted channels as primary fluid and at least a part of the reaction fluid heated in the reactor can be supplied to the secondary slotted channels as secondary fluid after reaction, so that reaction fluid can be preheated in the plate heat exchanger before entering the reactor by means of reaction fluids that have exited the reactor and been heated in the reactor.

The invention also relates to the use of a device according to the invention for heating reaction fluids to be supplied to a reactor for a high-temperature process, in particular for a cracking process, preferably of ammonia, or a reforming process, preferably of methane or LPG or naphtha or methanol or dimethyl ether, or a dehydration process, preferably of propane, by means of reaction fluids that have escaped from the reactor and have been heated in the reactor.

The invention further relates to a method for operating a plant according to the invention, comprising the steps

- at least one primary slit channel, preferably all primary slit channels, is supplied with a reaction fluid to be supplied to the reactor, in particular natural gas or dimethyl ether or MEOH or NH3, as a primary fluid,

- At least one secondary slit channel, preferably all secondary slit channels, is supplied with reaction fluid that has flowed through the reactor and exited the reactor again, so that reaction fluid is present in the slit channel before entering the reactor. Plate heat exchangers can be preheated using reaction fluids that have escaped from the reactor and are heated in the reactor.

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

In other words, the present invention proposes the use of a plate heat exchanger in a pressure shell as a feed effluent heat exchanger for high-temperature processes, such as steam reforming, autothermal reforming, steam cracking or ammonia cracking.

High-temperature processes are understood to mean, in particular, those with a reaction temperature of at least 700°C.

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.

According to the invention, a group of the fissure channels can be used to allow a reaction fluid to flow through it. This fluid is to be supplied to a reactor for a high-temperature process, or is supplied during operation, and is used to heat the reaction fluid before it enters the reactor. This group of fissure channels is referred to herein as primary fissure channels, and the reaction fluid to be heated, or the "feed", is also referred to as the "feed". The primary fluid can be supplied to these fission channels as, or is supplied to, the reactor as primary fluid during operation. According to the invention, heating can be achieved by recovering heat from the hot reaction fluid exiting the reactor, in other words, process fluid, such as process gas, which can flow through the second group of fission channels, the secondary fission channels, or flows through them during operation.

In other words, the primary fluid is the reaction fluid that is supplied to, or is supplied to, the reactor, while the secondary fluid is the reaction fluid exiting the reactor—in other words, the reaction fluid after the high-temperature process or after the reaction, for example, after a reforming process such as steam reforming, after a cracking process, or after a dehydration process. It is understood that the composition of the reaction fluid before the reactor can and usually will differ from the composition of the reaction fluid after the reactor, i.e., after the reaction. Nevertheless, the term "reaction fluid" is used consistently here for both the reaction fluid flowing into the reactor (i.e., the reaction fluid before the reaction) and the fluid flowing away from the reactor (i.e., the reaction fluid after the reaction).

The reaction fluid that is initially supplied to the primary slit channels as the primary fluid for preheating can be, for example, natural gas, dimethyl ether (DME), MEOH or NH3.

One could also say that the reactor, with its inlet and outlet for the reaction fluid, is fluidically connected between the primary and secondary sides of the plate heat exchanger, so that the reaction fluid flows over or over the plate heat exchanger. The heat is carried through the primary slit channels (i.e., the primary side) to the reactor and away from the reactor via the secondary slit channels (i.e., the secondary side), thus allowing process or reaction heat to be used for preheating.

According to the invention, the plate heat exchanger of the (respective) device is installed 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. Thus, the plate heat exchanger, or rather its channels, can be permeated by hot, pressurized reaction fluid that is conveyed to and from a high-temperature process. The plate heat exchanger can be of a comparatively simple design and therefore inexpensive. The reaction fluid flowing through the plate heat exchanger for heat recovery before and after the high-temperature process can have a high pressure and a high temperature without the need for a complex seal of the plate heat exchanger or the primary and/or secondary channels.

The system according to the invention can comprise one or more devices according to the invention. Accordingly, in addition to a first device, for which the primary slotted channels of the plate heat exchanger are fluidically connected to the inlet of the reactor on the outlet side, and the secondary slotted channels of the plate heat exchanger are connected to the outlet of the reactor on the inlet side, at least one further device can be provided. The primary slotted channels of the plate heat exchanger of the at least one further device The devices are then expediently connected fluidically to the primary slotted channels of the plate heat exchanger of the device, and the secondary slotted channels of the plate heat exchanger of at least one further device are connected to the secondary slotted channels of the plate heat exchanger of the device. In other words, several, in particular two, devices according to the invention, each with a plate heat exchanger, can be connected upstream or downstream. This allows for the separation of temperature levels. By way of pure example, it may be mentioned that two devices are present, wherein the primary sides of their plate heat exchangers are successively flowed through by reaction fluid to be heated before it enters the reactor in its heated state, and wherein the secondary sides of their plate heat exchangers are successively flowed through by hot reaction fluid exiting the reactor for heat recovery. Then the temperature level in the device fluidically closer to the reactor can be higher than in the further device. The outlets of the primary slotted channels of the plate heat exchanger of the device or at least one further device are fluidically connected to the inlets of the primary slotted channels of the plate heat exchanger of the device, for example via at least one line, and the inlets of the secondary slotted channels of the plate heat exchanger of the device or at least one further device are connected to the outlets of the secondary slotted channels of the plate heat exchanger of the device, for example via at least one line.

It is also possible for a device according to the invention to comprise two or more plate heat exchangers arranged together in the pressure vessel of the device. In other words, in addition to one plate heat exchanger, at least one further plate heat exchanger is then present. In this case, too, a separation of temperature levels is possible via two or more plate heat exchangers of a device. In this case, it is advantageous for the primary slots of the plate heat exchanger to be fluidically connected to the inlet of the reactor on the outlet side, and its secondary slots to be fluidically connected to the outlet of the reactor on the inlet side, while the primary slots of at least one further plate heat exchanger are fluidically connected to the primary slots of the plate heat exchanger, and the secondary slots of the at least one further plate heat exchanger are fluidly connected to the secondary slots of the plate heat exchanger. In other words, several, in particular two, plate heat exchangers can be connected upstream or downstream. The outlets of the primary slots of the plate heat exchanger or at least one further plate heat exchanger are then expediently fluidly connected to the inlets of the primary slots of the plate heat exchanger, for example via at least one line, and the inlets of the secondary slots of the plate heat exchanger or at least one further plate heat exchanger are connected to the outlets of the secondary slots of the plate heat exchanger, for example via at least one line.

Two devices or plate heat exchangers, or their primary and secondary sides, can be directly connected without any further components or elements in between, but in principle also via such components or elements.

If two or more devices or plate heat exchangers are present, further development can provide for their design to operate at different temperatures or temperature ranges. The devices or plate heat exchangers can, for example, consist of different materials – at least with regard to some components. For instance, the plate heat exchanger of a device for a higher temperature level could be made of ceramic, and the plate heat exchanger of a device for a higher temperature level could be made of other materials. The heat exchanger of at least one other device – or at least one other plate heat exchanger of a device – for a lower temperature level must comprise metal or at least consist partly of metal. The plate heat exchanger for the lower temperature level can therefore be made of a more cost-effective material.

Advantageously, the primary slotted channels and the secondary slotted channels of the plate heat exchanger, or in the case of several, of the respective plate heat exchanger, are not fluidically connected.

Furthermore, it has proven particularly advantageous in the (respective) device according to the invention if the primary and secondary slotted channels of the (respective) plate heat exchanger are arranged alternately, in other words, if a primary slotted channel alternates with a secondary slotted channel. This allows for particularly efficient heating of the reaction fluid by recovering heat from the hot reactor outlet fluid.

The primary and secondary slotted channels of the (respective) plate heat exchanger can, for example, be operated in counterflow, coflow, or cross-counterflow. The device or system according to the invention can be designed accordingly, in particular comprising lines for appropriate fluid flow.

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

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(s). The plate heat exchanger can be monitored for leaks using a leakage sensor. The leakage sensor for monitoring the (respective) plate heat exchanger is preferably located inside the pressure vessel. If the pressure vessel is or will be filled with, for example, an inert gas, it is advantageous to monitor for the primary gas or a component thereof. If the pressure vessel is filled with, for example, a primary gas, it is advantageous to monitor for the reaction product. In particular, leaks between secondary gap channels and the pressure vessel can be detected. This is also possible if the pressure in the pressure vessel is higher than the pressure in the secondary gap channels, as a partial pressure difference can be sufficient for this purpose. It should also be noted that leaks are tolerable to a certain extent without affecting the operation of the The device or system would have to be interrupted in this way. This is very advantageous, as, for example, somewhat larger error tolerances in manufacturing can be accepted.

In a further development, a catalyst material is provided in at least one of the primary slotted channels, preferably in all primary slotted channels of the plate heat exchanger or at least one plate heat exchanger, in particular a catalyst material for pre-cracking or pre-reforming. The plate heat exchanger can then be used not only for heating the feed by recovering heat from hot process fluid, but also for pre-reforming or pre-cracking, which has proven to be particularly suitable.

An optional catalyst material provided in the primary cracking channel(s) can be, for example, a nickel-based catalyst material, particularly for the (pre-)reforming of hydrocarbons. It can be a solid material on a support. Alternatively or additionally, it can be modified with precious metals. Such catalyst materials, as well as iron-based systems or bimetals, are also suitable, especially for the (pre-)cracking of NH3.

The catalyst material optionally provided in the primary slotted channel(s) can 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 means of a washcoat. For example, plates of the plate heat exchanger can be coated with the catalyst material or with a coating containing the catalyst material. The primary slit channels can be coated with a coating material. One or more insert plates, made of or coated with the catalyst material (e.g., with a washcoat), can also be arranged in the primary slit channels, which can simplify manufacturing. The catalyst material can also be present in the form of catalytically active structures. For example, catalytically active networks can be incorporated into the primary slit channels.

The device according to the invention is not an electrolytic device or an electrolytic reactor. In other words, it is specifically not a device in which electrically driven chemical reactions, particularly redox reactions forced by electrical energy, can or do take place. Accordingly, no electrolytic reactions are carried out in the primary or secondary slit channels within the framework of the method according to the invention.

Using at least one device according to the invention or within the framework of the method according to the invention, it can be provided, in particular, that the reaction fluid is heated on the primary side to a temperature of up to 800°C, preferably to a temperature in the range of 200°C to 800°C, and especially preferably in the range of 400°C to 800°C. The (respective) device or the (respective) plate heat exchanger can be designed accordingly. The inlet temperature of a reaction fluid to the (first) plate heat exchanger can, for example, be in the range of 200°C to 400°C.

Alternatively or additionally, it is possible to supply the at least one secondary slotted channel with reaction fluid at a temperature in the range of 700°C to 1200°C, preferably in the range of 750°C to 950°C. If several plate heat exchangers (of one or more devices) are present- This applies in particular to the at least one secondary slotted channel of the plate heat exchanger that is closest to the reactor outlet in terms of flow characteristics.

The device or devices according to the invention may include pressure control means which are designed and/or configured in such a way that the pressure difference prevailing during operation 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, can be adjusted, preferably controlled.

In an advantageous further development of the method according to the invention, the device or system 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 slotted channels, preferably in all primary slotted channels, which has proven to be particularly suitable. Alternatively or additionally, the device or system 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 slotted channels, and preferably in all primary slotted channels. In other words, when setting or controlling a maximum pressure difference between the interior of the pressure vessel and the pressure in one or more primary slotted channels, a percentage difference and/or absolute deviations can be used.

Pressure control means of the device or system 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 pressure in one or more primary slotted channels. The pressure of the pressure fluid can be adjusted during operation, for example, to match the pressure in the primary slotted channel(s). The pressure control devices can be designed and/or configured accordingly.

If the system according to the invention includes pressure control means, these can alternatively or additionally be designed and/or arranged in such a way that the pressure difference prevailing during operation between the pressure in at least one of the primary slotted channels, preferably in all primary slotted channels, and the pressure in at least one of the secondary slotted channels, preferably in all secondary slotted channels, can be adjusted, preferably controlled, by means of them.

However, a pressure difference can also exist – between the pressure in the primary and secondary slotted channels and/or between the pressure in the reactor and the pressure in the primary and/or secondary slotted channels – whereby (significantly) different pressures are also possible in principle. The secondary slotted channels, or the plates defining the secondary slotted channels, can then be welded together, or suitable seals and sufficient contact pressure of the plates can be implemented to allow for higher pressure differences. The same can apply alternatively or additionally to the primary slotted channels, or the plates defining the primary slotted channels.

It may also be provided that the primary and/or secondary slotted channels are equipped with stabilizing elements, in particular stabilizing ribs. These stabilizing elements can increase stability, especially in applications where larger pressure differences occur between the primary and secondary slotted channels. (can), it may be advantageous to reinforce the gap channels accordingly. Stabilizing elements, for example in the form of stabilizing struts, can extend between two adjacent plates and be supported by the adjacent plates.

In the event that a larger pressure differential occurs or is intended to occur during operation, for example, between primary and secondary channels—such as a pressure difference of more than 5 bar, or even significantly 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 pressed against at least one other element of the plate heat exchanger during operation due to the higher pressure on one side (primary or secondary).

In a further advantageous embodiment, the device according to the invention comprises a control unit 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 unit.

As a rule, the pressure in the primary slot channel(s) and the pressure in the primary fluid supply to the primary slot channels and/or in the primary fluid discharge from the primary slot channels are almost identical. This is especially true when there is a heat exchanger between the plate heat exchanger and the primary fluid supply to the primary slot channels. scher or whose primary slot channels and at least one supplying or discharging line no valve or similar device is arranged.

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 device according to the invention can comprise a primary differential pressure measuring device for measuring the pressure difference between the pressure in the pressure vessel and/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 provided, it can alternatively or additionally be configured to measure the pressure difference between the pressure in the pressure vessel and/or in at least one line upstream of it on the one hand, and the pressure in at least one line upstream of the 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 device 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 a or be connected to several of the primary slit channels, or via one or more additional 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 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.

Alternatively or additionally, a reactor pressure measuring device can be provided for the metrological recording of the pressure and/or pressure loss in the reactor.

The pressure measuring device and/or the primary pressure measuring device and/or the secondary pressure measuring device and/or the Pri- The primary differential pressure measuring device and/or the secondary differential pressure measuring device and/or the reactor pressure measuring device can be part of the pressure control means of the device or system according to the invention.

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 and/or the reactor 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.

The pressure fluid supply means can further be configured to generate an increased pressure in the pressure vessel in the range of 2 bar to 100 bar, particularly in the range of 5 bar to 100 bar, preferably in the range of 10 bar to 100 bar, and most preferably in the range of 20 bar to 100 bar. The pressure fluid supply means can also be configured to generate an increased pressure in the pressure vessel in the range of 2 bar to 40 bar, particularly in the range of 5 bar to 40 bar, preferably in the range of 10 bar to 40 bar, and most preferably in the range of 20 bar to 40 bar.

It has also proven particularly advantageous if the pressure control means, in particular a control device thereof, are designed in such a way and/or 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.

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 even if the aforementioned supply means each comprise at least one compressor and/or at least one pump and/or at least one valve, but this is by no means a requirement. In the simplest case, these can each consist of just a supply line or an 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 include or are provided by a primary inlet line, and the pressure fluid supply means include 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 reaction or feed fluid, in particular feed gas, which is supplied to the primary slotted channels for heating by recovering heat from the hot reaction fluid exiting the reactor, or a partial flow of this, 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 reaction fluid, which is supplied to the at least one primary slit channel as primary fluid, is also supplied to the pressure vessel as pressure fluid, preferably wherein the reaction fluid originating from a common source is supplied to the at least one primary slit channel and the pressure vessel as primary and pressure fluid, respectively. The device according to the invention can be designed and/or configured accordingly.

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

It can further be provided that the pressurized fluid and the primary fluid, which is in particular determined by the reaction 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 device according to the invention is characterized accordingly in that a pressure outlet line is provided through which pressure fluid can escape from the pressure vessel and that a primary outlet line is provided through which primary fluid, which has flowed through the primary slot channels, can escape 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, which is supplied by the reaction fluid, can also be supplied to the pressure vessel. The fluid is supplied to and discharged from the pressure vessel and recombined with the primary fluid that has flowed through and exited the primary slotted channels. The pressure inlet line can be configured as a first bypass line, branching off from the primary inlet line and leading to the pressure vessel, and the pressure outlet line can be configured as a second bypass line leading away from the pressure vessel and, in particular, emptying into the primary outlet line. Together, these form the bypass through which a portion of the reaction fluid is "captured," bypassed the primary slotted channels of the plate heat exchanger(s), and 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.

In an advantageous embodiment, the pressurized fluid can be cooled. The device 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 device according to the invention can comprise a pressure fluid circuit, in which excess pressure fluid can be discharged from the pressure vessel and returned to the pressure vessel.

In an advantageous embodiment of the device according to the invention, the (respective) plate heat exchanger can include a preferably electric heating device. For example, one or more plates of the (respective) plate heat exchanger can preferably be heated electrically by means of the heating device.

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 if the primary split channels are connected to each other 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, and each aligned hole forms a primary-secondary distribution or collector channel extending transversely through the plates and the defined gap channels between them, in particular a cylindrical channel. If four holes are provided in each plate, in particular a primary distribution channel and a primary collector channel as well as a secondary distribution channel and a secondary collector channel are formed or defined.

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 given 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 a given plate heat exchanger are identical in construction. The plates preferably consist of or comprise metal and/or ceramic. The same may apply to other components of the plate heat exchanger.

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 an advantageous embodiment, the plate heat exchanger can be provided with an insulating layer of thermally insulating material on its outer surface. This prevents excessive heating of the pressure vessel surrounding the plate heat exchanger(s) during operation. The plate heat exchanger(s) may also include a housing. In this case, the housing may, in particular, have an insulating layer made of a thermally insulating material.

The reactor of the system according to the invention can be designed as an electrically heated reactor.

The reactor can, in principle, be suitable for various high-temperature processes and designed accordingly. For example, a system according to the invention can include a reactor for a cracking process. It can also be a reactor for a reforming process, which can also be called a reformer, or a reactor for a dehydration process.

The reactor can be designed in particular for steam reforming or autothermal reforming of hydrocarbons, for example methane, LPG or naphtha, or for steam reforming or autothermal reforming of oxygenates, for example methanol or DME, or for cracking ammonia or for steam cracking of hydrocarbons or for a high-temperature dehydrogenation process.

Reactions that have proven to be particularly suitable within the scope of the present invention are:

- Steam reforming (preferably electrically heated) of hydrocarbons, for example methane, LPG or naphtha, or of oxygenates, for example methanol or DME (dimethyl ether), particularly with or at a reactor outlet temperature of 750 to 950°C and a pressure of up to 30 bar. In this case, the reaction fluid is transferred by means of the device according to the invention - or in the case Several devices – preferably preheated to up to 800°C. This can depend on the density of the reaction fluid and its vapor-to-carbon ratio.

- Autothermal reforming of hydrocarbons, for example methane, LPG or naphtha, or of oxygenates, for example methanol or DME, particularly with or at a reactor outlet temperature of 950 to 1050°C and a pressure of up to 70 bar. In this case, the reaction fluid is preferably preheated to up to 800°C using the device(s) according to the invention. This can depend on the density of the reaction fluid and its vapor-to-carbon ratio.

- Cracking of ammonia (NH3), wherein the reactor is preferably heated externally electrically or autothermally, particularly with or at a reactor outlet temperature of 750 to 1050°C and a pressure of up to 30 bar. In this case, the reaction fluid is preferably preheated to up to 800°C by means of the device(s) according to the invention. This can depend on the density of the reaction fluid and its vapor-to-carbon ratio.

- Steam cracking of hydrocarbons, particularly with or at a reactor outlet temperature of 700 to 950°C and a pressure of up to 2 bar. In this case, the reaction fluid is preferably preheated to up to 800°C using the device(s) according to the invention. This can depend on the density of the reaction fluid and its steam-to-carbon ratio.

- High-temperature dehydration processes, for example propane dehydration. In a further development, the system according to the invention can also include a cooling device for the reaction fluid, by means of which the reaction fluid exiting the reactor can be cooled before entering the secondary slit channels, in particular by supplying, or especially injecting, a cooling fluid, preferably water, to the reaction fluid. This can be a quench cooling device by means of which water can be injected.

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 system according to the invention in a purely schematic representation.

Figure 2 shows a perspective external view of the device according to the invention for heat transfer of the system from Figure 1 ,

Figure 3 is a purely schematic sectional view of the device of the system from Figure 1, and

Figure 4 shows a second embodiment of a system according to the invention in a purely schematic representation.

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

Figure 1 shows in a purely schematic representation a first embodiment of a system 1 according to the invention, comprising a reactor R and a The device V according to the invention is comprised. Figure 2 shows the device V of the system 1 in a perspective external view and Figure 3 a schematic sectional view of the device V.

The reactor R is designed as a reactor for a high-temperature process. In particular, it can be a reactor R for a (steam) cracking process or a reforming process, such as a steam reforming process or an autothermal reforming process, or for a dehydration process.

The device V can be used to heat the reaction fluid before it enters the reactor R. It can be heated to a temperature required for the high-temperature process that takes place in the reactor R during operation, in particular a temperature in the range of 400°C to 800°C. This heating is achieved by recovering heat from the hot reaction fluid exiting the reactor R, in other words, the process fluid.

The device V specifically comprises a plate heat exchanger 2 with a plurality of adjacent plates 3, in particular plates oriented at least substantially parallel to one another. In Figure 1, only a few of the plates 3 are shown by way of example, designated with the reference numeral 3. In the embodiment shown here, the plates 3, which are made of metal, all have a rectangular outer contour and the same dimensions; in other words, they are all the same size.

Between the plates 3, gap channels 4, 5 are defined, specifically one gap channel 4, 5 between each pair of adjacent plates 3. The gap channels 4, 5 are divided into two groups, namely several fluidically interconnected, specifically fluidically parallel, Pri- Primary slot channels 4, and several fluidically interconnected, specifically fluidically parallel, secondary slot channels 5. The slot channels 4 of one group, the primary slot channels 4, alternate with the slot channels 5 of the other group, the secondary slot channels 5. A primary slot channel 4 is therefore always located between two secondary slot channels 5, or – in the case of the leftmost primary slot channel 4 at the edge of the figure – next to a secondary slot channel 5. Similarly, a secondary slot channel 5 is always located between two primary slot channels 4, or – in the case of the rightmost secondary slot channel 5 at the edge of the figure – next to a primary slot channel 4.

Optionally, each of the primary slot channels 4 can contain a catalyst material 6 for pre-cracking or pre-reforming. In the highly simplified, purely schematic Figure 1, the catalyst material 6 is only indicated by way of example in some primary slot channels 4. Figure 1 schematically shows, by way of example, a granular catalyst material 6, even if only over a section of the respective primary slot channel 4. It is understood that the primary slot channels 4 can be filled with, for example, a granular catalyst material 6 along their entire length. Alternatively or additionally, it is also possible that the plates 3 are coated with catalyst material 6 or with a coating material containing catalyst material 6. One or more insert plates can also be arranged in the primary slot channels 4, which consist of the catalyst material or are coated with the catalyst material, for example by a washcoat, which can simplify manufacturing. It is also possible that the catalyst material is present in the form of catalytically active structures. For example, catalytically active networks may be provided in the primary and/or secondary slit channels. It should be noted that the internal structure of the plate heat exchanger 2, including the plates 3, primary and secondary gap channels 4, 5 and the catalyst material 6, is only recognizable in Figure 1, but is not shown again in Figure 2.

The device V further comprises primary fluid supply means 7 for supplying a primary fluid to the primary slot channels 4. The primary fluid is the reaction fluid that is to be supplied to the reactor R for the reaction taking place therein. This can be, for example, natural gas, DME, MEOH, or NH3. The primary fluid supply means 7 can 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 device V also includes secondary fluid supply means 10 for supplying a secondary fluid to the secondary slot channels 5. The secondary fluid supply means 10 can include at least one compressor and at least one valve, which are not shown separately in the purely schematic figure 1.

The secondary split channels 5 are - analogous to the primary split channels 4 - all connected on the input side to a central secondary distribution channel 11. technically connected, 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 outlet side of the secondary slotted channels 5, a secondary collector channel 15 is provided in an analogous manner, in which fluid exiting from all secondary slotted channels 5 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 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 means of recesses provided in the plates 3. For example, four recesses can be located in each plate 3. In particular, round holes (not shown in the figure) are provided, wherein the holes are located at identical positions in all plates 3 and the holes of all plates 3 are 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 in particular a cylindrical 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 gap channels, or the separation thereof, can then be achieved via seals (not shown), as is well known from conventional plate heat exchangers. The holes are preferably located in the edge region of the plates 3. If the plates 3 are rectangular, as in the illustrated embodiment, one of the holes can be located in or near each corner.

In the embodiment shown here, the primary and secondary slot channels 4, 5 are visibly flowed through in countercurrent flow (see also the arrows provided as examples in some of the slot channels 4, 5, which indicate the flow direction through the respective slot channel 4, 5). However, the primary and secondary slot channels can also be flowed through in cocurrent flow or cross-countercurrent flow.

The primary outlet line 14 of the plate heat exchanger 2 of the device V is fluidically connected to the inlet E of the reactor R, so that primary fluid, which has flowed through the primary slotted channels 4 for heating, can be supplied to the reactor R. The outlet A of the reactor R is further connected to the secondary inlet line 12, so that hot reaction fluid, which exits the reactor R, particularly at a temperature in the range of 750°C to 1050°C, can be supplied to the secondary slotted channels 5 for heat recovery. The reactor R is fluidically positioned between the primary and secondary sides of the plate heat exchanger 2 of the device V. It should be noted that the hot reaction fluid, particularly process gas, exiting the reactor R does not need to be completely introduced into the secondary slotted channels 5 of the plate heat exchanger 2, and usually is not. Rather, only a portion of the reaction fluid can be directed into the secondary side of the plate heat exchanger 2. A further portion can also be used for another purpose, which is not shown in Figure 1.

Furthermore, it should be noted that hot reaction fluid exiting reactor R can first be cooled before being fed to the secondary side of the plate heat exchanger 2 of the device V. For this purpose, the system 1 can include a cooling device Q for the reaction fluid, by means of which the reaction fluid exiting reactor R can be cooled before entering the secondary slotted channels 5. In the embodiment shown in Figure 1, a quench cooling device is specifically provided, by means of which water can be injected into the reaction fluid as needed to lower the temperature. The quench cooling device Q includes a valve II through which the water can be injected.

The device V 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 in the pressure vessel 18.

The pressure vessel 18 comprises an outer shell made of cost-effective steel, which is lined on the inside with an insulating layer of a thermally insulating material. The plate heat exchanger 2 is provided with thermal insulation. This thermal insulation ensures, or contributes to, a maximum operating temperature of 200°C, preferably 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 be provided with an insulating layer made 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 apparent 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 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 slot channels 4 is simultaneously used as the pressurized gas for the pressure vessel 18.

Cooling of the pressurized fluid can be provided. The device V 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 devices are provided which are designed and/or configured in such a way that the pressure differential occurring during the operation of the pre- direction V between the pressure in the pressure vessel 18 and the pressure in the primary slot channels 4 prevails, is adjustable, preferably controllable.

The device V, in particular the pressure control means, specifically comprises a control unit 24 by means of which the pressure prevailing in the interior 20 of the pressure vessel 18 can be adjusted, preferably regulated. The control unit 24 can also be used to adjust, preferably regulate, the pressure in the primary gap channels 4. For this purpose, the control unit 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 measuring the pressure in the pressure vessel 18 and/or the pressure in at least one primary slot channel 4. Alternatively or additionally, a primary differential pressure measuring device may be provided for measuring the pressure difference between the pressure in the pressure vessel 18 and the pressure in at least one of the primary slot channels 4. Alternatively or additionally, a pressure measuring device may 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 may be part of the pressure control system. The control unit 24 may be connected to the pressure measuring devices and/or the differential pressure measuring device to enable control or regulation based on the measured pressure values.

It should be noted that, alternatively or additionally to pressure measurement in the pressure vessel 18 or at least in a primary slotted channel 4 or secondary slotted channel 5, the pressure can also be measured in the supply- The pressure transfer can take place, specifically in at least one fluid-technically connected 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. In the case of differential pressure measurement, the focus can also be on the supply, specifically at least one line upstream of the pressure vessel 18 or at least one primary slotted channel 4 or secondary slotted channel 5.

Alternatively or additionally, pressure measurement can be performed in a feed 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 slot channels 5. Thus, at least one pressure measuring device, e.g., at least one pressure- A sensor 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, may be provided. 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.

A reactor pressure measuring device for the metrological recording of the pressure and/or pressure loss in the reactor R may also be provided.

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

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

During operation of plant 1, the reaction fluid for reactor R, for example natural gas, DME, MEOH or NH3, is supplied as the primary fluid to the primary channel 4, in other words, the primary side of the plate heat exchanger 2. Simultaneously, a pressurized gas is supplied to the pressure vessel, in this case also the reaction gas intended for reactor R, for example from the same source. It should be noted that the primary fluid can also be preheated before it enters the plate heat exchanger 2 of the device V, for example to 400°C. The system 1 can include an additional heat exchanger for such supplementary primary fluid preheating (not shown).

The secondary slotted channels 5 of the plate heat exchanger 2, which are fluidically connected to the outlet A of the reactor R via the secondary inlet line 12, are supplied with reaction fluid that has flowed through and out of the reactor R, in other words, reaction fluid after the reaction, and which can have a temperature in the range of 750°C to 1050°C. If necessary, the reaction fluid after the reaction can first be cooled somewhat by means of the quench cooling device Q before it enters the device V and the secondary slotted channels 5.

In the plate heat exchanger 2, heat is transferred from the hot reaction fluid flowing through the secondary side after reaction in the reactor R to reaction fluid that is supplied to the reactor R via or through the primary side of the plate heat exchanger 2, for example to 600°C.

The pressure prevailing in the pressure vessel 18 can be adjusted to the pressure in the primary slotted channels 4 by means of the control device 24.

In particular, it can be provided that the device V is operated such that the pressure in the pressure vessel 18, particularly with the aid of the control device 24, lies a maximum of 20%, more specifically a maximum of 10%, preferably a maximum of 5%, and most preferably a maximum of 1% above or below the pressure in the primary slotted channels 4. The device V can be operated such that the pressure in the pressure vessel The pressure in the primary slot channels 4 is located by a maximum of 5 bar, in particular by a maximum of 1 bar, preferably by a maximum of 100 mbar. The control device 23 is designed and/or configured accordingly.

Preferably, the system 1 is operated such that the pressure in the primary slotted channels 4, the pressure in the pressure vessel 18, and the pressure in the reactor R differ from each other 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%. Alternatively, the system can be operated such that the pressure in the primary slotted channels 4, the pressure in the pressure vessel 18, and the pressure in the reactor R differ from each other by a maximum of 5 bar, in particular by a maximum of 1 bar, and preferably by a maximum of 100 mbar.

Advantageously, a low pressure drop in reactor R, such as a cracker, reformer, or dehydrator, is ensured. This can be achieved, for example, by using a catalytic washcoat, a honeycomb or monolithic structure, or a catalyst packing with minimized pressure drop as an alternative to a particle catalyst bed.

The control unit 24 can be trained and/or configured accordingly.

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.

An optional leakage sensor, which can be located in pressure vessel 18, can monitor for a lack of gas. The leakage sensor It detects, in particular, a leak between secondary slot channels 5 and pressure vessel 18. This is also possible if the pressure in pressure vessel 18 is higher than in secondary slot channels 5, since even a partial pressure difference of the component is sufficient.

It should be noted that leaks can be tolerated to a certain extent without impeding the operation of the plant, and leakage monitoring may be provided but is not mandatory.

Optionally, the reaction fluid, particularly after flowing through the secondary channels 5 of the plate heat exchanger 2 and preheating the reaction fluid on the primary side, can be used for steam generation. The resulting steam can then be fed, for example, into a solid oxide electrolyzer cell (SOEC) to produce hydrogen. The hydrogen produced in this way can then be used, for example, to generate ammonia. Such a configuration has proven to be particularly efficient.

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

In particular, a bypass can be provided through which a portion of the reaction fluid is "tapped off" before entering the primary slot channels 4, fed to the pressure vessel 18, discharged from it, and recombined with the reaction fluid that has flowed through the primary slot channels 4. In the second outlet shown in Figure 4, In an exemplary embodiment of a system 1 according to the invention, such a bypass is provided in the device V. 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 reaction fluid is also supplied to the primary slot channels 4 as primary fluid, 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 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 pressure fluid (here also the reaction fluid) is recombined with the reaction fluid exiting the primary slot channels 4. The pressure 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 reaction fluid supplied to the primary slotted channels 4 as primary fluid bypasses the pressure vessel 18 via these 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 device V or system 1, via which its valve position can be adjusted. The valve position, in particular, determines how much of the primary fluid is guided through the pressure vessel 18 via the bypass 28, 30. This also determines, in particular, the degree to which the pressure vessel 18 is cooled by the primary fluid. A control unit 24, which can also be present in principle 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 not excluded that such a feature is additionally provided in the example from Figure 4 (not shown).

It should be noted that the device V according to Figure 4, in accordance with that of Figure 1, may optionally also have a pressure vessel outlet 24 and a safety valve 25 in addition to the second bypass line 29, which, however, is not shown in Figure 4 for the sake of clarity. It is also understood that it is possible, in principle, for a device V according to the invention to comprise not just one, but several plate heat exchangers 2 arranged in the pressure vessel 18 of the device V (not shown).

Reference symbol list

1 Annex

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

A Exit

E Input R Reactor

Q Cooling unit

U-valve

V Device

Claims

REQUIREMENTS 1. Device (V) for heat transfer 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 subdivided into several primary gap channels (4) which are fluidically connected, in particular fluidically connected in parallel, and several secondary gap channels (5) which are fluidically connected, in particular fluidically connected in parallel, wherein primary fluid supply means (7) are provided for supplying a primary fluid to the primary gap channels (4) and secondary fluid supply means (10) are provided for supplying a secondary fluid to the secondary gap channels (5), a pressure vessel (18) which surrounds the plate heat exchanger (2), pressure fluid supply means (19) which are configured to supply a pressure fluid to the pressure vessel (18) and in particular to supply it to the pressure vessel (18) to generate an increased pressure of at least 2 bar, in particular at least 5 bar, preferably at least 10 bar, particularly preferably at least 20 bar. 2. Device (V) 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 device (V) between the pressure in the pressure vessel (18) and the pressure in at least one of the primary slot channels (4), preferably in all primary slot channels (4), can be adjusted, preferably re- is gelable, 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 device (V) by a maximum of 20%, in particular by a maximum of 10%, preferably by a maximum of 5%, particularly preferably by a maximum of 1% above or below the pressure in at least one of the primary slot channels (4), preferably in all primary slot channels (4), and/or to maintain the pressure in the pressure vessel (18) during operation of the device (V) 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 slot channels (4), preferably in all primary slot channels (4). 3. Device (V) according to claim 2, characterized in that the pressure control means comprise a pressure measuring device for measuring the pressure in the pressure vessel (18) and/or the pressure in at least one line upstream of the pressure vessel (18) and/or in at least one line downstream of the pressure vessel (18), and a primary pressure measuring device for measuring the pressure in at least one of the primary slot channels (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), 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 slot channels (4) on the other. 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. 4. Device (V) according to one of the preceding claims, characterized in that the primary fluid supply means (7) comprise or are provided by a primary inlet line (9), 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. 5. Device (V) 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 slot channels (4), can exit 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. 6. Device (V) according to claims 4 and 5, 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). 7. Device (V) according to one of the preceding claims, characterized in that in at least one of the primary slot channels (4), be- preferably in all primary cracking channels (4), a catalyst material is provided, in particular a catalyst material for pre-cracking or pre-reforming. 8. Device (V) 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) can preferably be heated electrically by means of the heating device. 9. Device (V) 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). 10. Device (V) according to one of the preceding claims, characterized in that the plate heat exchanger (2) comprises steel and/or ceramic, and/or is provided on the outside with an insulating layer made of a thermally insulating material, and/or that the plates (3) of the plate heat exchanger (2) are at least substantially rectangular and/or have a structured surface on at least one side. 11. Device (V) 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 slit channels (4) and the secondary slit channels (5) are arranged alternately. 12. Device (V) according to one of the preceding claims, characterized in that the primary slot channels (4) and/or the secondary slot channels (5) are provided with stabilizing elements, in particular stabilizing ribs. 13. Device (V) 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). 14. Use of a device (V) according to one of the preceding claims for heating reaction fluids to be supplied to a reactor (R) for a high-temperature process, in particular for a cracking process, preferably of ammonia, or a reforming process, preferably of methane or LPG or naphtha or methanol or dimethyl ether, or a dehydration process, preferably of propane, by means of reaction fluids that have escaped from the reactor (R) and have been heated in the reactor (R). 15. Plant (1) comprising a reactor (R) for a high-temperature process, in particular a cracking process or a reforming process or a dehydration process, and a device (V) according to any one of claims 1 to 13, wherein the primary slit channels (4) are connected to an inlet (E) of the reactor (R) are fluidically connected and wherein an outlet (A) of the reactor (R) is fluidically connected to the secondary slotted channels (5) so that a reaction fluid to be supplied to the reactor (R) can be supplied to the primary slotted channels (4) as primary fluid and at least a part of the reaction fluid heated in the reactor (R) can be supplied to the secondary slotted channels (5) as secondary fluid after reaction, so that reaction fluid can be preheated in the plate heat exchanger (2) before entering the reactor (R) by means of reaction fluids that have exited the reactor (R) and have been heated in the reactor (R). 16. Plant (1) according to claim 15, characterized in that at least one further device (V) according to one of claims 1 to 13 is provided, wherein the primary slotted channels (4) of the plate heat exchanger (2) of the at least one further device (V) are fluidically connected to the primary slotted channels (4) of the plate heat exchanger (2) of the device (V) and wherein the secondary slotted channels (5) of the plate heat exchanger (2) of the at least one further device (V) are fluidically connected to the secondary slotted channels (5) of the plate heat exchanger (2) of the device (V). 17. Plant (1) according to claim 15 or 16, characterized in that the reactor (R) is designed as an electrically heated reactor, and/or that the reactor (R) is designed for steam reforming or autothermal reforming of hydrocarbons, in particular methane, LPG or naphtha, or for steam reforming or autothermal reforming of oxygenates, in particular methanol or DME, or for cracking ammonia or for steam cracking of hydrocarbons or for a high-temperature dehydrogenation process, in particular propane dehydrogenation. 18. Plant (1) according to one of claims 15 to 17, characterized in that a reactor pressure measuring device is provided for measuring the pressure and/or the pressure loss in the reactor (R), and/or that a cooling device (Q) is provided for the reaction fluid, by means of which reaction fluid exiting the reactor (R) can be cooled before entering the secondary slot channels (5), in particular by supplying, in particular by injecting, a cooling fluid, preferably water, to the reaction fluid. 19. Method for operating a plant according to any one of claims 15 to 18, comprising the steps - at least one primary slit channel (4), preferably all primary slit channels (4), is supplied with a reaction fluid to be supplied to the reactor (R), in particular natural gas or dimethyl ether or MEOH or NH3, as a primary fluid , - at least one secondary slot channel (5), preferably all secondary slot channels (5), is supplied with reaction fluid that has flowed through the reactor (R) and exited the reactor (R) as secondary fluid, so that the reaction fluid can be preheated in the plate heat exchanger (2) before entering the reactor (R) by means of reaction fluid that has exited the reactor (R) and been heated in the reactor (R), and - a pressure fluid, in particular a pressurized gas, is supplied to the pressure vessel (18), preferably wherein the pressurized gas comprises or consists of H2 and/or N2, particularly preferably a mixture of H2 and N2 or a mixture of H2 and CO2 or synthesis gas or primary gas. 20. Method according to claim 19, characterized in that the system (1) is operated such that the pressure in the pressure vessel (18) is reduced by 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 (4), preferably in all primary slotted channels (4), and/or that the system (1) is operated in such a way 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 (4), preferably in all primary slotted channels (4). 21. Method according to one of claims 19 or 20, characterized in that the reaction fluid supplied to the at least one primary slot channel (4) as primary fluid is also supplied to the pressure vessel (18) as pressure fluid, preferably wherein the reaction fluid originating from a common source is supplied to the at least one primary slot channel (4) and the pressure vessel (18) as primary and pressure fluid, 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. 22. Method according to one of claims 19 to 21, 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. 23. Method according to one of claims 19 to 22, characterized in that the reaction fluid in the at least one primary slit channel (4) is heated to a temperature in the range of 200°C to 800°C, preferably heated in the range of 400°C to 600°C, and/or that the at least one secondary slit channel (5) is supplied with reaction fluid at a temperature in the range of 700°C to 1200°C, preferably in the range of 750°C to 950°C.