WO2007101749A1 - Reacteur pour la realisation de reactions chimiques avec echange de chaleur - Google Patents

Reacteur pour la realisation de reactions chimiques avec echange de chaleur Download PDF

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Publication number
WO2007101749A1
WO2007101749A1 PCT/EP2007/050797 EP2007050797W WO2007101749A1 WO 2007101749 A1 WO2007101749 A1 WO 2007101749A1 EP 2007050797 W EP2007050797 W EP 2007050797W WO 2007101749 A1 WO2007101749 A1 WO 2007101749A1
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Prior art keywords
reactor according
reaction
sheets
reactor
thermo
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PCT/EP2007/050797
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German (de)
English (en)
Inventor
Simon Becht
Johannes Josef Albrecht
Andreas Geisselmann
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Evonik Degussa Gmbh
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Publication of WO2007101749A1 publication Critical patent/WO2007101749A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/248—Reactors comprising multiple separated flow channels
    • B01J19/249—Plate-type reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2451—Geometry of the reactor
    • B01J2219/2453—Plates arranged in parallel
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2451—Geometry of the reactor
    • B01J2219/2456—Geometry of the plates
    • B01J2219/2458—Flat plates, i.e. plates which are not corrugated or otherwise structured, e.g. plates with cylindrical shape
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2451—Geometry of the reactor
    • B01J2219/2456—Geometry of the plates
    • B01J2219/246—Perforated plates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2461—Heat exchange aspects
    • B01J2219/2462—Heat exchange aspects the reactants being in indirect heat exchange with a non reacting heat exchange medium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2469—Feeding means
    • B01J2219/247—Feeding means for the reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2476—Construction materials
    • B01J2219/2477—Construction materials of the catalysts
    • B01J2219/2479—Catalysts coated on the surface of plates or inserts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2476—Construction materials
    • B01J2219/2483—Construction materials of the plates
    • B01J2219/2485—Metals or alloys
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2491—Other constructional details
    • B01J2219/2492—Assembling means
    • B01J2219/2493—Means for assembling plates together, e.g. sealing means, screws, bolts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2491—Other constructional details
    • B01J2219/2492—Assembling means
    • B01J2219/2496—Means for assembling modules together, e.g. casings, holders, fluidic connectors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/245—Plate-type reactors
    • B01J2219/2491—Other constructional details
    • B01J2219/2498—Additional structures inserted in the channels, e.g. plates, catalyst holding meshes

Definitions

  • the present invention relates to a reactor, in particular a Plattenreak- gate for carrying out reactions with heat exchange. These are preferably heterogeneously catalyzed, strongly exothermic or endothermic gas phase reactions. Furthermore, the invention relates to a method for carrying out such chemical reactions in the reactor according to the invention.
  • the width of the reaction space can be set very precisely, whereby a very uniform flow distribution and thus a uniform residence time behavior can be realized.
  • the reactor according to the invention is particularly suitable for carrying out chemical reactions under conditions in which the reactant mixture is explosive.
  • the reaction space is formed by a narrow gap, which acts as a flame arrester, whereby a propagation of an explosion or even ignition of the gas mixture can be avoided, and on the other hand the reaction gap can be set very precisely must to ensure a uniform flow distribution.
  • Plate reactors with a plurality of mutually separated by plates alternately arranged reaction and heat transfer spaces are known from the prior art.
  • DE-A-198 48 208 and DE-A-197 54 185 describe plate reactors in which a plurality of cushion-like thermo-modules are arranged at a distance from one another, wherein the heat-exchange medium flows within the thermo-modules and is distributed between the thermo-modules. Modules a catalyst bed is arranged. Between the individual thermo modules no spacers are provided.
  • DE-A-100 42 746 describes a plate reactor with stacked thermo modules, wherein the reaction gap between two thermo modules is separated by spacers in the edge region of the modules. half of the reaction space is determined.
  • thermo modules are arranged in the shape of a pile and are guided in lateral grooves.
  • the nickela stau seh medium flows within the thermo modules and between the thermo modules a catalyst bed is arranged.
  • spacers in the form of cylinders through which a fastening bolt is pushed, can be introduced over the surface of the thermal modules, which spacers correspond to the spacing of the thermocouples.
  • holes must be provided for the implementation of the bolts in the thermocouples, which leads in particular when using thermo modules with plane-parallel sheets to increased sealing effort relative to the heat exchange space.
  • the production of such a plate reactor is very expensive, since the holes must be made for the implementation of the bolt with extremely tight tolerances.
  • DE-A-103 17 451 discloses plate reactors in which the reaction gap is defined by spacers in the form of webs between two adjacent plates.
  • the webs are formed as integral parts of the plates and the plates connected to each other via the webs.
  • This embodiment requires complex and expensive manufacturing processes. Furthermore, such joined reactors pose additional problems in coating the walls of the reaction space with catalysts. If the joining takes place before the coating, then only coating processes for closed structures, such as washcoat processes, are available. These are not suitable for setting precise layer thicknesses, both axially and laterally to the flow direction. The layer thickness is usually limited to areas under 100 ⁇ m. borders. If the coating of the catalyst before joining, the prepared catalyst is usually significantly thermally and mechanically loaded in the subsequent joining. For many catalysts this is expected to cause damage.
  • EP-A-1 234 617 describes plate reactors with reaction and heat transfer spaces separated from one another by thermoplates, in which the catalyst is applied in the form of a thin layer on at least part of the entire surface of the thermoplates which faces the reaction space.
  • a corrugated module is introduced into the reaction space. From the description it can only be seen that this should increase the catalyst area per volume. There is no question of setting a defined distance between two plates. This is also not possible because such corrugated structures can easily be deformed under pressure, resulting in undesirable catalyst flaking. To act as a spacer such corrugated modules would have to be made very solid in order to resist deformation.
  • a reactor with a plurality of mutually separated by sheets alternately arranged reaction ons- and heat transport spaces with close tolerance of the gap width of the reaction chamber over the entire surface of the reaction space, especially with very small gap widths and large exchange surfaces in manufacturing technology to provide a simpler way of reacting by a strongly exothermic reaction can be operated safely and chemical reactions can be carried out under conditions in which the reactant mixture is explosive.
  • reaction spaces with catalyst coating simple production without thermal or mechanical loading of the catalyst and reusability of the reactor with spent catalyst coating and simple recovery of noble metal-containing catalyst coatings should be possible.
  • a reactor for carrying out chemical reactions with heat exchange comprising a plurality of mutually separated by sheets, alternately arranged reaction and heat transport spaces, wherein the reaction spaces are bounded by two sheets, which by a plurality of over the surface
  • the spacers are distributed to the plates kept at a defined distance from each other, without being firmly connected to each other via the distance body.
  • the reactor according to the invention are prefabricated thermo modules that form the bounded by two sheets heat transfer space arranged in a stapeiförmig and are held by the spacer body in the defined distance from each other, whereby between two sheets of adjacent thermal modules of the reaction space is formed.
  • the plates forming the reaction space are not fixedly connected to one another via the spacer bodies, the plates or thermal modules and the spacer bodies can be manufactured independently of one another in a simple manner with high dimensional accuracy. Since the distance of the plates forming the reaction spaces is defined by the dimension of the spacer bodies, a very small tolerance of the reaction space width over the entire exchanger surface can thus be realized in a simple manner. Since the plates forming the reaction space are not connected to one another via the spacer bodies, it is not necessary to connect the plates to one another or to the spacer bodies, for example by thermal methods, such as soldering or welding.
  • thermo modules which can be easily coated with catalyst and then using the spacers in a defined distance from one another to form a reactor.
  • the thermo modules are preferably detachably connected to one another in such a way that the reaction chambers, with the exception of openings for the inlet and outlet of the reaction media, are sealed to the outside. That is, in a preferred embodiment, the connection points of the thermal modules can be reopened by suitable separation methods.
  • the spacer bodies are arranged in opposing depressions in the plates bounding a reaction space. It is particularly advantageous if the size and geometry of the recess and arranged therein spacer body are coordinated to give a conclusive or flexible fit.
  • This embodiment leads to a significantly simplified assembly of the reactor according to the invention.
  • the spacers can be temporarily fixed in the depressions of a sheet bounding the reaction space, for example by a wax, and the second sheet bounding the reaction space can be simply placed on the spacers.
  • the spacer body is a rolling element, for example, has the geometry of a ball or a cylinder, and the recesses in the opposite sheets have a corresponding geometry, such as plate or cup-shaped geometry in the event that the spacer body is a ball is. Then the second plate does not have to be aligned accurately, but can simply be placed on the spacer body and then brought by sliding or rolling in the intended position. Furthermore, the allowed Use of rolling elements as a spacer body a slight displacement of the plates into each other, which, for example, thermal stresses can be reduced.
  • the geometry and size of depressions of spacer bodies are matched to one another, so that a defined distance between the sheets forming the reaction space arises.
  • a ball as a spacer body with a cup-shaped recess, shell and ball have approximately the same radius or the fit can be flexible, if, for example, a ball with a dish-shaped recess, ie the radius the depression is much larger than that of the sphere used.
  • Flexible fits offer the advantage of increased mobility of the plates against each other, for example, to reduce thermal stresses.
  • the distance of the reaction space forming plates is no longer clearly defined.
  • the spacers may also have the geometry of a cuboid.
  • a cuboidal embodiment can consist of extended strips which can measure the entire reaction space and which can then form reaction channels, for example, for which a seal between them is not absolutely necessary.
  • a double-sided connection-free arrangement of the spacer bodies between the sheets forming the reaction space is preferred.
  • the spacers between the sheets usually do not perform a sealing function.
  • a force transfer via the spacer body is usually only in so far as it is necessary for a bias of the reactor for pressure stabilization.
  • the reactor is composed of a stack of pressure-resistant and rigid thermo modules.
  • the distance between two respective thermo modules is defined by spacer bodies, which are preferably located in depressions of two opposing thermal modules.
  • the gap between Two thermo modules form the reaction space, while the heat transfer medium is guided inside the thermo module.
  • thermo module consists of two sheets, which are preferably arranged plane-parallel in a defined distance from each other.
  • the thickness of the sheets is preferably in a range between 0.5 and 2 mm.
  • sheet is used for a sheet material having the required thermal conductivity and the required mechanical and thermal stability. Within these limits, the material of the sheets is freely selectable and is preferably a metal, with steel and aluminum, especially stainless steel, is particularly preferred.
  • the sheets are substantially planar, but in the preferred embodiment discussed above, e.g. structures formed by embossing, wherein the elevation of a structure is directed towards the other, the thermo module forming sheet and the lowering of this structure, the above discussed in connection with a preferred embodiment depression forms.
  • the shape of the structure may have various geometries as discussed above. It is preferred to select geometries for the structures formed by forming processes, such as forming. Embossing can be made in a particularly precise, simple and cost-effective manner.
  • the depth of the structures is preferably 0.1 to 10 mm.
  • cylindrical plate-like, dish-shaped to almost hemispherical or rectangular structures are preferred. Particularly preferred are plate, shell to almost hemispherical structures, which are then preferably used together with spherical spacers.
  • thermo module forming sheet The inwardly directed elevations of at least one embossed structure of a sheet may, but need not, be in contact with the base surface or with a protrusion of an embossing structure of the other, the thermo module forming sheet.
  • the two, a thermo module forming sheets can then be connected in one embodiment via the contact point (s), preferably by soldering, welding, gluing or riveting together.
  • the internal structure of the thermomodules which goes beyond the embossing, can in principle be freely selected. It makes sense to use structures that allow an effective and even heat exchange with the reaction chamber and ensure mechanical stability.
  • the thermo modules have further internal structural elements.
  • spacers such as cylindrical or cuboid, prefabricated body, which are positioned in a suitable form evenly in the space between the sheets.
  • the height of these spacers is equal to or greater than the minimum distance defined by the embossing pattern.
  • An arrangement in the form of laterally limited channels is conceivable, but not required.
  • the spacers inside the thermo modules are connected to both sheets by suitable joining methods, such as welding, soldering, gluing or riveting.
  • the function of the spacers within the thermal modules consists in the additional mechanical stabilization and the appropriate guidance of the heat carrier.
  • the position and size of the individual embossed structures and optional spacers is calculated based on the expected pressure differences between the process and the heat transfer medium side. If spacers are used, the density of embossed structures can be significantly reduced. Usually, all the reaction chambers are within the reactor according to the invention, or all heat transport spaces, each at the same pressure level.
  • the preferred thermal module according to the present invention in the edge region by a suitable operation, such as forming the plate edges or inserting strips in combination with a joining process, such as welding or soldering, permanently sealed.
  • a suitable operation such as forming the plate edges or inserting strips in combination with a joining process, such as welding or soldering, permanently sealed.
  • the sheet metal edges are laterally moved so that they already form the lateral boundary in the subsequent assembly to the thermal module and can be connected and sealed by welding. But it is also a seal by pressing against a seal possible, this is preferably to introduce before joining the embossing and spacer structures.
  • the finished joined and sealed thermo module is thus a stable, rigid and pressure-tight sandwich. It is capable of overpressing to absorb cess- or heat transfer medium without deforming it.
  • the distribution of the heat carrier within the thermo module may preferably be uniform and is achieved by a suitable positioning and design of the embossed structures and the optional spacers and the position of the inlet and outlet points.
  • the apparatus has a catalytic coating in the reaction space. This is usually applied to both outer sides of the thermo module. But it is also possible that only one side of the thermo module carries a catalyst. Another possibility is that a suitably placed on the thermo module sheet is coated, which then creates a positive, but not cohesive contact, between catalyst layer and thermo module.
  • An advantage of this embodiment is the easy separability of catalyst and thermal module.
  • the catalyst layer is chosen in thickness so that mass and heat transfer restriction are significantly lower than in a conventional catalyst bed, on the other hand, however, sufficient catalyst per area is accommodated in order to achieve a most economical embodiment.
  • the layer thickness tolerance is low, preferably ⁇ 15%.
  • Typical layer thicknesses are between 50 .mu.m and 2 mm, preferably between 200 .mu.m and 1 mm.
  • the layer has sufficient porosity to ensure good catalytic activity. Typical porosities are in the range 5-80%.
  • the layer can be produced by various known methods, such as spraying, screen printing, casting, knife coating or washcoating.
  • the above-mentioned optional recesses can be ensured by masking during coating. alternatives It is also possible to insert bodies into the depressions, which are removed again after coating.
  • the catalyst can be chosen freely according to the needs of the reaction, provided that a mechanically stable layer can be produced.
  • Examples of possible catalysts include:
  • Precious metals on oxides essentially of Al, Si, Ti and / or Zr optionally with addition of promoters o elements of the iron group on oxides essentially of Al, Si, Ti and / or Zr optionally with the addition of promoters o copper chlorides on oxides substantially of Al, Si, Ti and / or Zr optionally with the addition of promoters
  • the reactor can thus be thermally controlled very precisely.
  • the optimal process point can be adjusted with regard to temperature, pressure and the stoichiometric (or superstoichiometric) educt ratios. It can be used very highly active catalysts, since local overheating can be excluded.
  • the distance between the two sheets forming the reaction space eg the distance between two thermo modules and the catalyst layer thickness, if a catalyst coating is used, are preferably adjusted so that the free space of the reaction space is in the range of 20 to 3000 ⁇ m, preferably 300 to 1000 ⁇ m.
  • the reaction spaces are sealed to the outside with the exception of openings for the inlet and outlet of the reaction media.
  • the thermal modules along the outer edge are joined by known methods such as welding or soldering.
  • strips can be inserted to bridge the gap distance, or the thermal modules already contain an element that allows a good connection to the adjacent thermo module.
  • This joining can be done at a sufficient distance from the optional catalyst layer, e.g. avoid thermal damage to the catalyst.
  • a gasket with pressure can be used.
  • a preferred embodiment of the apparatus provides that the thermal modules are arranged together so that the joint between the modules can be reopened by suitable separation processes. In this way it is ensured that the reactor can be reused and the contained catalyst can be removed for recycling or disposal.
  • the supply and removal of the reaction medium is ensured by the already mentioned openings in the reaction chamber.
  • the uniform distribution within a reaction gap, at right angles to the flow direction is ensured process-dependent by the corresponding structuring and dimensioning of the inflow and outflow region. This is usually done by an artificially generated, or predetermined by the design, flow resistance.
  • individual components of the reaction medium can be supplied separately.
  • a mixing structure is expediently integrated into the reaction chamber at the inlet region of the components.
  • the mixture can also be carried out in a structure immediately in front of the reactor.
  • the structure should be dimensioned so that an explosion does not occur or can not propagate. The same applies to the combination of mixed structure and reaction space.
  • thermo modules or a part of the thermo modules have reactant channels, via which some or the entirety of the reactants can be metered into the reaction space.
  • the heat transfer leading portion in the thermo module is interrupted by such reactant leading channels.
  • the reactant channels are closed tightly against the heat carrier leading area.
  • the channels are connected via openings in the sheet to one side or both sides of the reaction space. These openings can be designed for example in the form of holes or slots.
  • the size is preferably chosen so that a sufficient pressure loss ensures uniform metering over the area of all openings (in the case of bores a diameter of approximately 100 ⁇ m-500 ⁇ m).
  • a possible catalyst layer can be interrupted at the level of the reaction channel, in particular in the region of the metering openings.
  • the thermo module may contain several such reactant channels. These are preferably mounted transversely to the flow direction in the reaction space.
  • the thermo module preferably contains a reactant channel at the inflow edge.
  • the reactant channels described can be used, for example, to generate highly reactive or explosive mixtures in the reaction space.
  • the main part of the components can be added via the normal inlet openings into the reaction space, while the component initiating the actual reaction is metered in via a reactant channel.
  • An arrangement with several reactant channels also allows a subsequent metering of components, for example if they are initially added in a deficit.
  • hoods By positioning the inflow and outflow region of the reactor can be operated in the DC, counter and cross-flow principle.
  • the supply and removal of reactants and heat transfer media preferably takes place via hoods ("headers"), which are preferably firmly connected to the reactor by a joining process such as welding or soldering, for example.
  • headers preferably contain already mentioned structures for uniform distribution of the media.
  • at least 4 headers are necessary, but depending on the number of inlet or outlet openings both in the reaction chamber and in the heat transfer area, it can also be any number. connected, which ensure the integration of the reactor in the process periphery.
  • headers As an alternative to the use of headers but also a separate connection of the individual reactor and heat transfer spaces to distribution or bus lines, for example. possible via flanges. It is also possible to connect certain media streams via headers and other media streams in parallel via individual connections.
  • the reactor is preferably designed so that larger pressure differences between two adjacent reaction spaces are avoided, so that at most small forces are effective.
  • the forces due to the pressure difference between the heat carrier space and the reaction space are largely absorbed by the internal structure of the thermo module.
  • the forces on the two outermost thermal modules by the pressure difference between the reaction space and the environment are preferably compensated by appropriately sized pressure plates, which are e.g. can be connected by tie rods that can be provided with a bias.
  • the tie rods can be provided with flexible force transducers such as e.g. Be provided plate springs.
  • the outermost thermal modules are designed so massive that they themselves can be used as pressure plates.
  • the entire reactor can be arranged in an outer pressure vessel, so that the external pressure can be adapted to the pressure in the reaction space.
  • thermo module surface contact between outer thermo module and pressure plate is possible.
  • This surface contact can be interrupted at the recesses, but it is also possible to dispense with the outermost thermo module on one side depressions.
  • the contact between the outer thermo module and the pressure plate takes place via spacer bodies arranged in the depressions of the module, which may be identical to those in the reaction spaces. Preferably, these are balls.
  • this external thermo module due to the possibly applied pressure difference forces act, if necessary, increase the density of the spacer body to prevent deformation of the thermo module.
  • the advantage of this preferred embodiment is that the spacer body allow rolling or sliding between the outer thermal module and pressure plate, so that mechanical stresses, eg due to an uneven temperature distribution during heating or cooling, can be reduced.
  • Another advantage lies in the reduced heat conduction between the thermal module and pressure plate, which can otherwise provide heat removal from the system.
  • the pressure plate can be replaced by an external thermo module, which is designed so massive that a deformation is also omitted.
  • Another means for avoiding thermally induced stresses is the careful isolation and optionally heating of the pressure plates.
  • Another part of this invention is the use of a reactor described above in the various embodiments for carrying out chemical reactions. These are preferably strongly exothermic or endothermic processes. Particular preference is given to gas-phase processes and very particularly preferably to partial oxidations, examples being:
  • these processes are operated under conditions in which the reactant mixtures are explosive under reaction conditions.
  • the reactor according to the invention must be designed so that the gap defining the reaction space is smaller than the Zündg. Erase distance of the respective reaction mixture under the given conditions. Furthermore, it must be ensured by means of suitable process control or by means of corresponding internals (for example diffusion barrier) that no explosive mixture of the educts and / or products can enter the macroscopic region before the reactor inlet or after the reactor outlet.
  • FIG. 1 shows an embodiment of a thermo-module according to the invention in an exploded view.
  • FIG. 2 shows a schematic representation of an embodiment of an outer termination of the thermo-module stack of the reactor according to the invention.
  • FIG. 3 shows a schematic representation of the arrangement of two thermal modules according to the invention.
  • FIG. 4 shows different embodiments of depressions according to the invention in the metal sheets forming the reaction space with matching spacer body geometries.
  • FIG. 5 shows a schematic representation of the stacking of thermal modules according to the invention.
  • FIG. 6 shows a schematic representation of the material flows through the reactor according to the invention.
  • thermomodule 14 suitable for the reactor according to the invention shown in FIG. 1
  • a plurality of dish-shaped depressions are provided in the metal sheets 5 forming the main surfaces of the thermo module.
  • the recesses 2 are formed by embossing structures, wherein the elevations of these embossed structures are directed inwards and form in the embodiment shown in Figure 1 contact points 6, where the two sheets 5, which form the thermo module 14, are interconnected.
  • the main surfaces of the thermo module are provided with a catalytic coating 8, wherein only the coating is shown on one side.
  • the catalytic coating 8 has corresponding recesses in the region of the depressions 2.
  • the sheets forming thermal modules 14 are connected to one another via the contact points 6 between two opposite elevations of the embossing structures forming the recess for the spacers, as well as by spacers 7 To ensure thermal modules.
  • the distance between two thermal modules, which defines the reaction space, is defined by the geometry of the recesses 2 and the spacer body 1.
  • the surfaces of the stacked thermal modules 14 delimiting the reaction space 3 are provided with a catalytic coating 8, whereby are recessed in the wells 2 for receiving the spacer body 1.
  • the outer end of the reactor according to the invention forms a pressure plate 11.
  • the contact between the outer thermo module 14 and the pressure plate 11 takes place via spacer bodies 13 arranged in the recesses 2 of the module 14, which are identical to those in FIG may be the reaction chambers 3.
  • the density of the spacer bodies 13 is increased in comparison to the density of the spacer bodies 1 in the reaction space 3 in order to better absorb the forces due to the increased pressure difference between the reaction space 3 and the surroundings.
  • FIG. 3 shows a preferred embodiment of the thermal modules 14 for the reactor according to the invention.
  • the thermo modules are formed by two plane-parallel arranged sheets 5, which are connected to one another both by spacers 7 and via the contact point 6 of two opposite elevations of the recess 2 forming the spacers 1 embossing structure.
  • the depressions 2 have a shell-shaped geometry.
  • the spacer bodies 1, which define the distance between the thermal modules 14, have a cylindrical geometry which tapers conically to the recesses 2 in the thermal modules 14 at the ends.
  • the thermo modules 14 have reactant channels 9, via which reactants can be metered into the reaction space.
  • the heat transfer chamber 4 in the thermo module 14 is interrupted by the reactant channels 9.
  • the reactant channels are connected via openings 10 in the embodiment shown in FIG. 3 to one side with the reaction space 3.
  • FIG. 4 shows various embodiments of the geometry of the depressions 2 in the thermal module 14 and the geometries of the spacer bodies 1 matching thereto.
  • a plurality of thermal modules 14 are arranged in the form of a stack in the form of a stack.
  • the reaction space 3 is defined by the distance between two thermal modules 14, which is determined by the geometry of the depressions 2 and the spacer body 1 is.
  • the sheets 5 of the thermocouples shown in Figure 5 are connected to each other both via the spacers and through the contact points on the recesses 2 and have reactant channels 9.
  • Figure 6 shows schematically a possible material flow guide for the reactants and streams, the product stream and the heat transfer stream. As shown in FIG. 6, the respective material streams are fed or removed from the reactor via hoods (headers) 12.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

La présente invention concerne un réacteur destiné à la réalisation de réactions chimiques avec échange de chaleur, comprenant une pluralité de zones de transport de chaleur (4) et de réaction (3) disposées de manière alternée, séparées les unes des autres par des plaques métalliques (5), chacune des zones de réaction (3) étant limitée par deux plaques métalliques (5), lesdites plaques étant maintenues à une distance définies les unes par rapport aux autres par une pluralité d'espaceurs (1) distribués à la surface des plaques métalliques (5), sans être liées fermement les unes aux autres par l'espaceur (1), ainsi qu'un procédé de réalisation d'une réaction chimique, notamment fortement exothermique, dans le réacteur selon l'invention.
PCT/EP2007/050797 2006-03-03 2007-01-26 Reacteur pour la realisation de reactions chimiques avec echange de chaleur WO2007101749A1 (fr)

Applications Claiming Priority (2)

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DE102006010368.8 2006-03-03
DE200610010368 DE102006010368A1 (de) 2006-03-03 2006-03-03 Reaktor zur Durchführung chemischer Reaktionen mit Wärmeaustausch

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102011081786A1 (de) 2011-08-30 2013-02-28 Wacker Chemie Ag Verfahren zur Acetoxylierung von Olefinen in der Gasphase
KR101800070B1 (ko) 2011-06-06 2017-11-21 아르끄마 프랑스 현장 주입 플레이트형 반응기
EP3531053A1 (fr) * 2018-02-26 2019-08-28 Commissariat à l'énergie atomique et aux énergies alternatives Réacteur échangeur comportant des canaux d'injection et de répartition de réactifs
WO2024030439A1 (fr) 2022-08-05 2024-02-08 Celanese International Corporation Catalyseur destiné à l'acétoxylation d'oléfines
WO2024030440A1 (fr) 2022-08-05 2024-02-08 Celanese International Corporation Charge de zone de catalyseur et procédés d'acétoxylation d'oléfines l'utilisant

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Publication number Priority date Publication date Assignee Title
DE1542304A1 (de) * 1964-06-16 1970-04-30 Marston Excelsior Ltd Chemischer Reaktor
EP1147807A2 (fr) * 2000-04-19 2001-10-24 DEG Engineering GmbH Réacteur pour la conversion catalytique de réactifs, en particulier de réactifs gazeux
DE10221016A1 (de) * 2002-05-11 2003-11-27 Ballard Power Systems Reaktor
DE102005022958B3 (de) * 2005-05-19 2006-07-20 Forschungszentrum Karlsruhe Gmbh Mikrostrukturreaktor und Verwendung desselben

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1542304A1 (de) * 1964-06-16 1970-04-30 Marston Excelsior Ltd Chemischer Reaktor
EP1147807A2 (fr) * 2000-04-19 2001-10-24 DEG Engineering GmbH Réacteur pour la conversion catalytique de réactifs, en particulier de réactifs gazeux
DE10221016A1 (de) * 2002-05-11 2003-11-27 Ballard Power Systems Reaktor
DE102005022958B3 (de) * 2005-05-19 2006-07-20 Forschungszentrum Karlsruhe Gmbh Mikrostrukturreaktor und Verwendung desselben

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR101800070B1 (ko) 2011-06-06 2017-11-21 아르끄마 프랑스 현장 주입 플레이트형 반응기
DE102011081786A1 (de) 2011-08-30 2013-02-28 Wacker Chemie Ag Verfahren zur Acetoxylierung von Olefinen in der Gasphase
WO2013030073A1 (fr) 2011-08-30 2013-03-07 Wacker Chemie Ag Procédé d'acétoxylation d'oléfines en phase gazeuse
US8907123B2 (en) 2011-08-30 2014-12-09 Wacker Chemie Ag Process for the acetoxylation of olefins in the gas phase
EP3531053A1 (fr) * 2018-02-26 2019-08-28 Commissariat à l'énergie atomique et aux énergies alternatives Réacteur échangeur comportant des canaux d'injection et de répartition de réactifs
FR3078394A1 (fr) * 2018-02-26 2019-08-30 Commissariat A L'energie Atomique Et Aux Energies Alternatives Reacteur echangeur comportant des canaux d'injection et de repartition de reactifs
WO2024030439A1 (fr) 2022-08-05 2024-02-08 Celanese International Corporation Catalyseur destiné à l'acétoxylation d'oléfines
WO2024030440A1 (fr) 2022-08-05 2024-02-08 Celanese International Corporation Charge de zone de catalyseur et procédés d'acétoxylation d'oléfines l'utilisant

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