DE102017125018A1 - Process for the formation and catalytic conversion of a reactant mixture and reactor with appropriate mixing chamber - Google Patents

Abstract

A reactor (100) is proposed for the formation and catalytic conversion of a gaseous educt mixture, the reactor (100) having a first chamber (1), a second chamber (2) and a third chamber (3), the first chamber ( 1) is delimited from the second chamber (2) by means of a fluid-permeable separating structure (4) and the second chamber (2) is arranged between the first chamber (1) and the third chamber. It is provided that the fluid-permeable separation structure (4) longitudinal elements (5) which are arranged parallel to each other and with gaps (6) between each other, and extending parallel to a plane (7) between the first chamber (1) and the The second chamber (2) extending longitudinally, wherein at least a part of the longitudinal elements (5) each have longitudinal channels (8) each having a plurality of openings (9), each in one or more of the interstices (6) open. A corresponding method is likewise an object of the present invention.

Description

The present invention relates to a process and a plant for the formation and catalytic conversion of a starting material mixture according to the respective preambles of the independent claims.

State of the art

In a series of chemical processes, reactant mixtures are catalytically reacted. These can be in the form of ignitable gas mixtures and are then fed below their auto-ignition temperature of the catalytic conversion. In the following, an "ignitable gas mixture" is understood to mean a gas mixture which comprises one or more oxidizable components, in particular one or more hydrocarbons, but also compounds such as, for example, hydrogen or hydrogen sulfide, and also oxygen. The oxygen may be added, for example, in the form of air or pure oxygen. An ignitable gas mixture has a composition which makes it possible to ignite the gas mixture by means of an ignition source. As also explained below, only occasionally ignitable gas mixtures can be present in corresponding processes, for example in a start-up operation, in process deviations and the like. Such an ignitable gas mixture formed only intermittently can also be fed to the catalytic reaction as starting material mixture.

The present invention is i.a. Example, the oxidative dehydrogenation (ODH) of alkanes having two to four carbon atoms described in which the alkanes are fed together with oxygen as the starting material mixture of a catalytic reaction zone of a reactor. A corresponding starting material mixture can in principle be ignitable. In particular, the invention can be used in the ODH of ethane (so-called ODH-E), but in principle also in the ODH higher alkanes such as propane and butane. However, the invention can also be used and advantageous for other processes in which gaseous reactant mixtures are catalytically reacted, for example in other oxidation processes such as the synthesis of ethylene oxide or acrylic acid.

The ODH, especially the ODH-E, may be advantageous over more established processes for producing alkenes such as steam cracking or catalytic dehydrogenation. Thus, there is no thermodynamic equilibrium limitation due to the exothermicity of the reactions involved. Basically, no regeneration of the catalysts is required because the presence of oxygen allows in situ regeneration. Finally, in contrast to steam cracking, smaller amounts of worthless by-products such as coke are formed.

For further details regarding the ODH is to relevant literature, for example Ivars, F. and Lopez Nieto, JM, Light Alkanes Oxidation: Targets Reached and Current Challenges, in: Duprez, D. and Cavani, F. (ed.), Handbook of Advanced Methods and Processes in Oxidation Catalysis: From Laboratory to Industry , London 2014: Imperial College Press, pages 767-834 , or gardener, CA et al., Oxidative Dehydrogenation of Ethanes: Common Principles and Mechanistic Aspects, Chem. Cat. Chem., Vol. 5, No. 11, 2013, pages 3196 to 3217 , referenced.

In the case of ODH and other processes in which ignitable gas mixtures can be formed at least temporarily, unwanted ignition may occur in the presence of an ignition source upstream or in the catalytic reaction zone of a reactor. The subsequent, largely uncontrolled burning without further measures can be explosive, deflagrative or detonative.

An explosion is an uncontrolled burn-up of an ignitable gas mixture with a laminar flame front. In a deflagration there is a turbulent flame front. Explosions or deflagrations on the one hand and detonations differ essentially by the speed of propagation. In an explosion or deflagration this is below, in a detonation typically well above the speed of sound. An explosion or deflagration can turn into a detonation after a certain start-up length and a minimum concentration of fuel and oxygen. Explosions, deflagrations and detonations of gas mixtures lead to a massive increase in pressure, which can lead to bursting of the equipment used and corresponding consequential damage.

In the case of an explosion or deflagration of a stoichiometric mixture of alkanes, alkenes and air, a pressure increase by a factor of ten or an explosion or deflagration of a stoichiometric mixture of alkanes, alkenes and oxygen can lead to a pressure increase by a factor of 20. In the case of a detonation again much higher pressure increases are effected.

If an explosion is mentioned below, the corresponding explanations also extend to deflagration. Accordingly, "explosion-proof" arrangements or explosion protection measures also provide protection against deflagration.

It is possible, in principle, to avoid corresponding mixing states, ie the formation of ignitable gas mixtures, and to take measures in this connection which make it possible to reliably exclude the formation of ignitable gas mixtures also during startup and shutdown as well as during process deviations. Furthermore, it is possible to operate corresponding methods at low pressure and the equipment used explosion-proof, possibly even detonationsfest execute. In this context, alternatively or additionally, safety-related discharge measures or discharge means, for example rupture disks or explosion protection flaps, can be used.

In principle, however, with regard to the reaction behavior, the product spectrum or the selectivity and / or in view of downstream product processing, however, the catalytic conversion of an ignitable gas mixture as educt mixture may be desirable or unavoidable, or it may be advantageous in certain constellations if no exclusion of the formation of flammable gas mixtures is required in all circumstances. In such cases, therefore, the avoidance of the formation of ignitable gas mixtures is not possible or at least disadvantageous under the aspects mentioned. The explosive or detonation-resistant design of systems or the provision of appropriate discharge measures or discharge means leads to additional costs.

The object of the invention is to provide measures which make it possible to safely enable the formation and, if appropriate, catalytic conversion of corresponding gas mixtures which can be present at least temporarily in an ignitable state without undesired ignition and subsequent explosion or deflagration or detonation.

Disclosure of the invention

Against this background, the present invention proposes a reactor and a process for the catalytic conversion of a gaseous starting material mixture and a corresponding plant with the features of the independent patent claims. Embodiments are each the subject of the dependent claims and the following description.

The present invention is based on a reactor or process for the formation and catalytic conversion of a gaseous reactant mixture in which at least one first gas or gas mixture and a second gas or gas mixture are mixed to form the educt mixture. The educt mixture is fed to its catalytic reaction of a reaction zone of the reactor.

Examples of catalytic reactions have already been explained above. As mentioned, the process according to the invention is suitable in particular for use in ODH (E) reactors or corresponding processes in which a reaction zone of a reactor is fed with an alkane and oxygen-containing gas mixture as reactant mixture. However, as mentioned above, the present invention can also be used, for example, in the abovementioned other processes or in all processes in which gaseous reactant mixtures are to be catalytically reacted and an ignitability is present or can not be ruled out from the outset.

In principle, the reaction zone in the context of the present invention may be equipped with any desired catalysts, in particular in immobilized form. For example, in the context of the present invention, fixed-bed catalysts, honeycomb bodies or catalytically active bodies can be used in externally heated and / or cooled pipes. In the case of a tube reactor, for example, a number of reaction tubes are filled with catalyst. These are passed through a reactor chamber and heated or cooled therein. By suitable distribution devices, the starting material mixture is distributed to the individual reaction tubes, as also explained below.

If this is the case that an education and a catalytic conversion of a gaseous Eduktgemischs takes place or this gas mixture is fed to a reaction zone of a reactor, this, as previously explained, not necessarily understood that in the context of the entire process is constantly an ignitable gas mixture must be formed and reacted as the starting material mixture. In particular, in the context of the present invention, only at certain times, i. For example, in the starting operation of a corresponding reactor or when switching between different operating modes or operating deviations, come to form ignitable gas mixtures. In a control operation, however, the reaction zone, for example, a non-ignitable gas mixture can be supplied as a starting material mixture, for example. Conversely, a non-flammable mixture can also be driven only near or at the selected operating point, while non-flammable conditions are selected during start-up or operating change, for example by increased dilution with inert gases.

The ignitability of a corresponding gas mixture is determined by its composition, in particular its content of oxidizable compounds and oxygen, absolutely and in relation to each other. In particular, contains a corresponding ignitable gas mixture Hydrocarbons as in the case of the ODH alkanes. In addition to the first and the second gas mixture, other gas mixtures can also be used and mixed in the context of the present invention.

In particular, in the context of the present invention, the first gas or gas mixture may contain one or more oxidisable compounds, in particular alkanes or alkenes. The second gas or gas mixture may in particular contain oxygen. In principle, it is also possible that the first gas or gas mixture contains the oxygen and the second gas or gas mixture contains the one or more oxidizable compounds. The gas or gas mixture containing the oxygen in each case can be pure oxygen, air or oxygen-enriched air or mixtures thereof. Generally, both gases may contain other inert or less reactive diluents, such as water vapor, nitrogen, methane, carbon dioxide or other components, independent of the source of oxygen. The term "inert" refers to the reaction behavior of corresponding compounds in a corresponding reaction system and is not limited to classically referred to as "inert" compounds such as the inert gases nitrogen, helium or argon.

In principle, it is also possible within the scope of the present invention to provide the first and / or the second gas or gas mixture already as a gas or gas mixture which contains one or more oxidizable compounds and at the same time oxygen. In this way, possibly a miscibility of the first of the second gas or gas mixture can be improved. Even if, for example, the first or the second gas mixture is provided completely or partially as a recycle stream, this may also contain oxygen in addition to one or more oxidizable compounds. In contrast to the reactant mixture formed using the first and the second gas or gas mixture, however, in such a first or second gas mixture, it may be easier to ensure an ignitability at any time.

In the context of the present invention, a reactor is provided which is set up for the formation and catalytic conversion of a gaseous reactant mixture. The reactor comprises a first chamber, a second chamber and a third chamber, wherein the first chamber is delimited from the second chamber by means of a fluid-permeable separation structure and the second chamber is arranged between the first and the third chamber. Such a reactor typically has an at least partially cylindrical outer shell, so that the first chamber, the second chamber and the third chamber are each at least partially cylindrical and at least partially have identical cross sections. A cylinder axis extends through the first chamber, the second chamber and the third chamber, wherein the fluid-permeable separation structure is arranged in particular perpendicular to the cylinder axis between the first chamber and the second chamber.

It is understood that, as explained in more detail below, the separation structure also has an extension in the direction of this cylinder axis, so that it is arranged between two planes, of which a first plane to the first chamber and a second plane to the second chamber has. The first and second planes are arranged parallel to one another and at a defined distance, which defines the thickness of the fluid-permeable separation structure.

As also explained in more detail below with reference to the method according to the invention, in particular a first gas or gas mixture is fed via the first chamber, which experiences in particular a fluid rectification or flow uniform distribution via the fluid-permeable separation structure in the manner explained below. Typically, this first gas or gas mixture can be fed into the first chamber via a feed line, which may also be arranged concentrically to the cylinder axis, but typically has a smaller cross-section than the first chamber. This typically results in a flow non-uniformity of the first gas or gas mixture in the first chamber, which is at least partially eliminated by the fluid-permeable separation structure. The first gas or gas mixture therefore flows with largely homogenized fluid flow via the fluid-permeable separation structure into the second chamber.

As also explained below, a second gas or gas mixture can be fed in particular by elements of the fluid-permeable separation structure, this second gas or gas mixture escaping, in particular, from channels arranged in the separation structure or their elements into interspaces of these elements. In this way, a particularly rapid and safe mixing of the second gas or gas mixture via corresponding channels in the first gas or gas mixture, which flows from the first chamber via gaps between the elements of the fluid-permeable separation structure into the second chamber, are effected. Even at the intervals between the elements of the fluid-permeable separation structure itself, but at the latest in the second chamber, this results in a particularly good mixing of the two gases or gas mixtures. In particular, a backflow is avoided, as also explained below.

In principle, the first gas or gas mixture or the second gas or gas mixture may be an oxygen-containing gas or gas mixture, the other gas or gas mixture then each having the oxidizable component. Further embodiments for this purpose have already been explained above. It is particularly advantageous if the gas or gas mixture fed into the first chamber and passing into the second chamber via the fluid-permeable separating structure is the one with the higher mass flow.

Starting from the second chamber and thus after mixing, the educt mixture formed in this way is transferred into the third chamber, which is formed as a reaction chamber and equipped with a corresponding catalyst. A catalyst can be provided in any desired manner, for example in the form of a fixed bed, in the form of honeycomb bodies or in the form of catalytically active bodies in externally heated and / or cooled tubes, as already mentioned above. Therefore, in the context of the present invention, the second chamber may be delimited by suitable means from the third chamber, for example via a suitable tube sheet.

In the context of the present invention, it is now provided that the fluid-permeable separating structure comprises longitudinal elements which are arranged parallel to one another and with gaps between them, and which extend longitudinally parallel to a plane between the first chamber and the second chamber. The longitudinal elements thus have a longitudinal extent, whose direction is arranged parallel to said plane. A "longitudinal extent" indicates the direction in which the longitudinal elements have the greatest length. The longitudinal extent is thus oriented perpendicular to the cylinder axis mentioned several times, around which the first chamber, the second chamber and the third chamber can be arranged. In other words, the fluid-permeable separating structure is in the form of a longitudinal grid, which is arranged between the first chamber and the second chamber, and which allows a passage of fluid from the first chamber into the second chamber via the intermediate spaces between the longitudinal elements.

As already mentioned, at least some of the longitudinal elements each have longitudinal channels, each having a plurality of openings, each opening into one or both adjacent intermediate spaces. Corresponding longitudinal channels can thus be connected to a feed line for providing the second gas or gas mixture, so that the second gas or gas mixture via the longitudinal channels and their openings in the space or between the longitudinal elements directly into the interstices and thus into the flowing through these spaces first gas or gas mixture can be fed or mixed. By such an arrangement, a particularly effective mixing can be achieved, as mentioned, backflow of ignitable gases or gas mixtures can be avoided against the flow direction in the direction of the first chamber. Furthermore, the use of the arrangement proposed according to the invention makes the formation of regions which are not or poorly perfused in the flow direction downstream of the fluid-permeable separation structure, i. in the second chamber, avoided.

By the inventively proposed reactor or its specific configuration can be achieved that all functions of flow equalization or homogenization, mixing and other functions from a reaction engineering and safety point of view can be combined. In the reactor there is an almost complete uniform distribution of the flow over the entire area flowed through and a uniform distribution of the second gas or gas mixture in the first gas or gas mixture at a short mixing distance, wherein a backflow of ignitable mixture against the flow direction and a formation of non or poorly traversed areas is avoided.

According to the invention, provision is made in particular for the first chamber to be acted upon by the first gas or gas mixture already mentioned several times, the second chamber being able to be fed in via the interspaces, and the longitudinal channels being able to be acted upon by the second gas or gas mixture mentioned several times, via the openings and the spaces in the second chamber can be fed. As mentioned, results in this way a particularly effective mixing and safety-favorable flow. A "longitudinal channel" extends in particular along at least part of the longitudinal extent of the respective longitudinal elements.

According to the invention it is provided in particular that at least a part of the longitudinal elements have pairs facing each other, which are formed by end faces of the longitudinal elements. In this context, "mutually assigning regions" are understood in particular to be those wall regions or end surfaces of longitudinal elements which, when viewed from above, project one above the other along a plane in which the axes are arranged which define the respective longitudinal extension of the longitudinal elements. These mutually adjoining areas thus lie between the first and second levels, which are partly mentioned above, wherein the first level assigns the first chamber and the second level assigns the second chamber and the first and second levels second level are arranged at a distance parallel to each other. The first and the second plane define a maximum extent of the longitudinal elements in the direction of the first and second chamber. In each case, said end surfaces of the longitudinal elements define an entry region for fluid into the intermediate spaces between the longitudinal elements, a free flow region and an exit region into the second chamber. Preferably, these sections initially taper and then widen again in the direction of the second chamber.

A corresponding taper is formed in particular in that the end faces from the direction of the first plane in the direction of the second plane each comprise a curved first end face and a flat second end face adjoining this first end face curved. As a result of the curvature of the curved first end surfaces, a distance between these end surfaces decreases increasingly starting from the first chamber in the direction of the second chamber. The free flow area, which is then defined by planes of the second end face, preferably does not change its cross section.

In other words, the pairs of second end faces facing each other in the embodiment of the present invention just explained are advantageously arranged parallel to one another and at a distance d from one another. This distance d is defined in particular on the basis of fluidic considerations in a suitable manner and in coordination with the respective other dimensions of the longitudinal elements and the corresponding distance. In this case, provision is made in particular for a corresponding inflow region, which is defined by the curved end surfaces, to be designed to minimize pressure loss. The distance d may in particular be 5 to 50 mm, preferably 15 to 25 mm.

Advantageously, therefore, the respective first end surfaces facing each other in pairs are each in the form of a quarter cylinder with a radius r, which is related to the distance d according to r = n × d, where n is 0.1 to 5, in particular 0.5 , Instead of providing a corresponding curved first end surface, only one edge break can also be made in each case. If curved first end faces are provided in the illustrated embodiment, an axis of the quarter cylinder extends in each case in the direction of the longitudinal extension of the longitudinal elements and thus perpendicular to the cylinder axis mentioned several times through the first, second and third chambers.

The free flow region defined by the second end surfaces arranged parallel to one another is advantageously selected such that the flow is applied to the wall in a correspondingly formed channel and thus a backflow and a diffusive backmixing are effectively suppressed.

In particular, the repeatedly mentioned end faces may comprise third end faces adjoining the second end faces from the direction of the first plane in the direction of the second plane. In this way, the mentioned channel expands between the second end surfaces arranged in parallel to form a larger clear width, which is formed or defined by the third end faces, which can likewise be arranged in particular parallel to one another.

In the embodiment of the present invention just described, the return in each case defines a parallel offset with a value t between the second termination surface and the third termination surface, wherein the value t is related to the distance d according to t = q × d, where q is 0, 25 to 2.5, in particular 0.5. As explained below, the second gas or gas mixture can be mixed in in particular via the third end face and the openings of the longitudinal channels opening out here in the longitudinal elements. This takes place in a region in which the corresponding channels have widened or already widened in the form of the intermediate spaces, so that a back pressure and thus a backflow is prevented.

As mentioned, a length of the free flow area between the second planes is advantageously optimized. In this case, a length in which a corresponding free flow can take place is chosen in a suitable manner. This is done in the context of the present invention in particular in that a distance between the first plane and the return is chosen such that it is the value I, where I is related to the distance e according to l = s × d, where s 0 , 5 to 25, in particular 10.

As an alternative to the configuration just described, with the return between the second plane and the third plane, it is also possible to provide that the end surfaces from the direction of the first plane in the direction of the second plane are in each case continuously adjacent to the second end surface, in the direction of the second plane include curved third end surfaces. The curvature can be designed in particular in the form of a semi-ellipse or a parabolic function. In this way, if necessary a further increase in the flow properties can be achieved, but in such an embodiment, if necessary, an increased manufacturing outlay arises.

In all of the embodiments explained above, it can be provided that the openings of the longitudinal channels open alternately in the third end faces on both sides of the longitudinal elements. In this way, a particularly advantageous interference is achieved because a corresponding gas mixture can be evenly distributed even more. An opening of the openings can be directed in a direction of 90 ° to the flow in the spaces se in, however, it can be an angle of 15 ° to 90 ° formed with the flow. Corresponding angles can be provided regardless of whether an alternating or non-alternating arrangement of the openings is provided.

As already explained several times, the first chamber can in particular be fluidically connected to a first fluid feed line and the longitudinal channels can in particular be fluidically connected to a second fluid feed line. The first gas or gas mixture can be fed in via the first fluid feed line and the second gas or gas mixture can be fed via the second fluid feed line.

The inventively proposed method for forming catalytic reaction of a gaseous reactant mixture comprises that a first and a second gas or gas mixture are mixed to the educt mixture and then fed to a reaction zone of a reactor and catalytically reacted there.

According to the invention it is provided that in a corresponding method, a reactor is used, as has been previously explained in different embodiments. In this case, according to the invention, the first gas or gas mixture is fed via the first chamber, the second gas or gas mixture is fed via the longitudinal channels and their openings, and the first gas or gas mixture and the second gas or Gesgemisch be in the interstices and / or the second chamber mixed to the educt mixture. The third chamber is used as the reaction zone and is therefore designed in a suitable manner, for example, provided with a corresponding catalyst.

According to a particularly preferred embodiment of the present invention, an average flow velocity at the narrowest point of the interstices between the longitudinal elements, which can be achieved by a suitable geometrical configuration, is set to be higher than the laminar flame velocity, higher than the turbulent flame velocity a quarter to half the speed of sound, in particular at about one third of the speed of sound, or at the speed of sound. In this way, in particular a backflow can be avoided.

In the context of the present invention, it may further be provided, in particular, that a residence time of the educt mixture is set such that it is less than the ignition delay time of the educt mixture. The ignition delay depends on the temperature, the pressure and the composition of the educt mixture. The residence time refers in particular to a residence time in the second chamber, in which basically an ignition is possible.

Further aspects and advantages of the method proposed according to the invention result from the previously explained features and advantages of the reactor according to the invention in a corresponding manner, so that reference is expressly made to these.

A further embodiment of the present invention may comprise providing the second chamber, ie the mixing zone of a corresponding reactor, with an inert or already catalytically active bed in order to minimize the mass of reactive gas and to increase the inert mass.

In particular, in this way, in the context of the present invention, a startling explosion energy can be withdrawn by a corresponding bed, so that the burn goes out. Thus, the required design pressure can be significantly reduced and the pressure jacket can be performed accordingly cheaper.

Instead of an inert bed, a structured packing and / or a static mixing element may be provided for the same purpose. Also by the thermal mass of a structured packing or a static mixing element energy can be withdrawn from a starting explosion. The structured packing, which may for example be formed from correspondingly structured metal sheets, or a static mixing element may in particular also be arranged only in a part of the second chamber. By means of a structured packing or a static mixing element, an improved mixture of the first and the second gas mixture in the mixing chamber or the corresponding area can additionally be achieved.

Instead of an explosion-proof design of the mixing zone, ie the second chamber, this can also be equipped with gas-discharging measures, for example with rupture disks to the environment or to a discharge system. Unsafe flow-through edge zones on the edge of a corresponding reactor can in particular be provided with a sheet metal sheet and executed in a technically sealed manner or, for example, an inert medium or a process medium, but which is not in particular the gas or gas mixture contained in each case.

The present invention will be explained in more detail below with reference to the accompanying drawing, which illustrates a preferred embodiment of reactors according to the invention and their parts.

list of figures

• 1A illustrates a reactor according to an embodiment of the invention in a simplified schematic longitudinal view and in partial view.
• 1B shows a simplified and enlarged cross-section along a sectional plane AA through the in 1A shown reactor.
• 1C illustrates a simplified and enlarged section along a sectional plane BB through the in 1A shown reactor.
• 2 Figure 3 illustrates an alternative embodiment of longitudinal elements of a separation structure for a reactor according to an embodiment of the invention.
• 3A illustrates longitudinal elements for a separation structure for a reactor according to an embodiment of the invention in a pseudo-perspective view.
• 3B FIG. 3 illustrates a longitudinal channel through a longitudinal element of a separation structure for a reactor according to an embodiment of the invention, with a section in the sectional plane CC in FIG 3A ,

In the figures, corresponding elements are given identical reference numerals and will not be explained repeatedly for the sake of clarity. If a reactor according to the invention is explained below, the corresponding explanations apply equally to a process carried out with this reactor according to an embodiment of the present invention.

Detailed description of the drawings

In 1A is a reactor according to an embodiment of the invention in a simplified schematic partial view in the form of a longitudinal section along an axis illustrated by dash-dotted lines and shown in partial view. The reactor or its in 1A shown part is in total with 100 designated.

The in 1 represented reactor 100 includes in the example shown a first chamber 1 , a second chamber 2 and a third chamber 3 , where the first chamber 1 in particular as a feed chamber for feeding a first gas or gas mixture, via a first fluid feed line 17 is provided, the second chamber 2 as a mixing chamber for mixing the first gas or gas mixture with a second gas or gas mixture via a second fluid feed line 18 is provided, and the third chamber 3 is used as the reaction chamber, wherein the third chamber 3 is provided in particular with a suitable catalyst, as previously explained several times.

The first chamber 1 and the second chamber 2 are by means of a fluid-permeable separation structure 4 separated from each other and the second chamber 2 is located between the first chamber 1 and the third chamber 3 ,

Details regarding the fluid-permeable separation structure 4 are illustrated in particular with reference to the following figures or sub-figures. The fluid-permeable separation structure is in the reactor 100 arranged such that it is parallel to a plane, which is shown here by dashed lines and designated 7, between the first chamber 1 and the second chamber 2 extends longitudinally.

1B shows a cross-sectional view of the in 1A illustrated reactor according to the sectional plane AA , in the 1A is designated accordingly. As in particular from 1B can be seen, comprises the fluid-permeable separation structure 4 each longitudinal elements 5 that are parallel to each other and with gaps 6 are arranged between each other. As in particular from a synopsis of 1A and 1B As can be seen, the longitudinal elements extend parallel to the plane 7 between the first chamber and the second chamber.

Further details regarding the fluid-permeable separation structure 4 or the longitudinal elements 5 arise from the 1C , which is an enlarged and only partial sectional view according to the sectional plane BB in 1A illustrated. Here are two of the longitudinal elements 5 (one of them only in partial representation) with a gap formed between them 6 illustrated.

As in particular from the 1C can be seen, have the longitudinal elements shown here 5 while each longitudinal channels 8th on, in turn, each openings 9 each having in one of the interstices 6 lead. As also from the 1C can be seen, the longitudinal elements shown here 5 A pair of facing each other areas, which are designated here in total by 10, and which, as illustrated here, in each case between one of the first chamber 1 assigning first level 15 and one of the second chamber 2 assigning second level 16 which is aligned parallel to the first plane extend. The mentioned levels are shown here dotted. They define the maximum extent of the longitudinal elements 5 in the direction of the first and second chambers 1,2.

As in 1C only on the longitudinal element shown on the right 5 Illustrates include these termination surfaces 10 doing so from the direction of the first level 15 towards the second level 16 each a curved first end surface 11 and a second termination surface adjacent to this plane 12 , It closes a third end surface 13 on, via a corresponding return (without a separate name), the parallel offset of the second end face 12 and the third endface 13 Are defined. The openings 9 the longitudinal channels 8th lead in particular in the area of this third end face.

While doing so in the in 1C illustrated embodiment, corresponding recesses and flat end surfaces 12 and 13 are provided in 2 an alternative embodiment is shown opposite to 1C only partially provided with reference numerals. Here, too, joins the second end surface 12 a third endface 13 but here is the second endface 12 continuously in the third end surface 13 passes over and the third closing surface 13 as explained above is curved.

In 3A is a pseudo-perspective view of a partially cut longitudinal member shown 5 , especially in the 1A to 1C illustrated embodiment illustrated, illustrated. As in particular from 3A As can be seen, the openings open 9 the longitudinal channels 8th in the third closing areas 13 , How out 3B can be seen, which is a sectional view through the cutting plane CC according to 3A illustrated, while these openings 9 alternate, ie on both sides of the longitudinal elements 5 lead.

QUOTES INCLUDE IN THE DESCRIPTION

This list of the documents listed by the applicant has been generated automatically and is included solely for the better information of the reader. The list is not part of the German patent or utility model application. The DPMA assumes no liability for any errors or omissions.

Cited non-patent literature

• Ivars, F. and Lopez Nieto, JM, Light Alkanes Oxidation: Targets Reached and Current Challenges, in: Duprez, D. and Cavani, F. (ed.), Handbook of Advanced Methods and Processes in Oxidation Catalysis: From Laboratory to Industry , London 2014: Imperial College Press, pp. 767-834 [0005]
• C.A. et al., Oxidative Dehydrogenation of Ethanes: Common Principles and Mechanistic Aspects, Chem. Cat. Chem., Vol. 5, No. 11, 2013, pages 3196 to 3217. [0005]

Claims (15)

Reactor (100) for the formation and catalytic conversion of a gaseous starting material mixture, wherein the reactor (100) has a first chamber (1), a second chamber (2) and a third chamber (3), wherein the first chamber (1) by means of a fluid-permeable separation structure (4) from the second chamber (2) is delimited and the second chamber (2) between the first chamber (1) and the third chamber is arranged, characterized in that the fluid-permeable separation structure (4) longitudinal elements (5) which are arranged parallel to each other and with spaces (6) between each other and which extend longitudinally parallel to a plane (7) between the first chamber (1) and the second chamber (2), at least a part of the longitudinal elements (5 ) each having longitudinal channels (8) each having a plurality of openings (9), each in one or more of the intermediate spaces (6) open. Reactor (100) according to Claim 1 in which the first chamber (1) can be acted upon by a first gas or gas mixture which can be fed into the second chamber (2) via the intermediate spaces (6) and in which the longitudinal channels (8) can be acted upon by a second gas or gas mixture is that on the openings (9) and the intermediate spaces (6) in the second chamber (2) can be fed. Reactor (100) according to Claim 1 or 2 in which at least part of the longitudinal elements (5) have pairs of facing areas (10) formed by end faces (11-13) of the longitudinal elements (5) extending longitudinally along the longitudinal elements (5) and between them a first plane (15) facing the first chamber (1) and a second plane (16) facing the second chamber (2) aligned parallel to the first plane (15). Reactor (100) according to Claim 3 in that the end faces (11-13) from the direction of the first plane (15) in the direction of the second plane (16) each comprise a curved first end face (11) and a flat second end face (12) adjoining the same. Reactor (100) according to Claim 4 in which the second end faces (12) facing each other in pairs are arranged parallel to one another and at a distance d from one another. Reactor (100) according to Claim 5 in which the respective first end faces (11) facing each other in pairs are in the form of a quarter-cylinder with a radius r, which is related to the distance d in accordance with r = n × d, where n is from 0.1 to 5, in particular 0 , 5, is. Reactor (100) according to Claim 5 or 6 in that the end surfaces (11-13) furthermore comprise third end surfaces (13) adjoining the second end surfaces (12) from the direction of the first plane (15) in the direction of the second plane (16). Reactor (100) according to Claim 7 in which the return respectively defines a parallel offset with a value t between the second termination surface (12) and the third termination surface (13), the value t being related to the distance d according to t = q × d, where q is 0, 25 to 2.5, especially 0.5. Reactor (100) according to Claim 6 or 7 in which the distance between the first plane (15) and the return is I, where I is related to the distance d according to I = s × d, where s is 0.5 to 25, in particular 10. Reactor according to one of the Claims 1 to 6 in that the end surfaces (11-14) also extend from the direction of the first plane (15) in the direction of the second plane (16), respectively, continuously adjoining the second end surface (12) and curved away from each other in the direction of the second plane (16) third end surfaces (13) include. Reactor (100) according to one of Claims 7 or 10 in which the openings (9) of the longitudinal channels (8) open alternately in the third end surfaces (13) on both sides of the longitudinal elements (5). A reactor (100) according to any one of the preceding claims, wherein the first chamber (1) is fluidly connected to a first fluid feed line (17) and the longitudinal channels (8) are fluidly connected to a second fluid feed line (18). Process for the formation and catalytic conversion of a gaseous reactant mixture, in which a first and a second gas or gas mixture are mixed to the educt mixture and then fed to a reaction zone of a reactor (100) and catalytically reacted there, characterized in that as the reactor (100) a reactor (100) according to any one of the preceding claims is used, wherein the first gas or gas mixture via the first chamber (1) is fed, wherein the second gas or gas mixture via the longitudinal channels (8) and their openings (9) is fed, the first gas or gas mixture and the second gas or gas mixture in the interstices (6) and / or the second chamber (2) are mixed into the reactant mixture, and wherein the third chamber (3) is used as the reaction zone. Method according to Claim 13 in which a mean flow velocity at the narrowest point the clearance is set to be higher than the laminar flame speed, higher than the turbulent flame speed, at a quarter to half the speed of sound or at the speed of sound. Method according to Claim 13 or 14 in which a residence time of the educt mixture in the second chamber (2) is set to be less than an ignition delay.

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