DE10254845A1 - Integrated reactor - Google Patents

Abstract

An integrated reactor with at least two spatially separated channel structures for guiding at least two fluid streams is presented, with a reaction taking place in at least one fluid stream within a reaction region, which causes a heat tone, and at the same time heat transfer between the fluid streams takes place. At least one further fluid can be metered into at least one of the at least two fluid streams distributed over the entire reaction area.

Description

The invention relates to an integrated Reactor according to the preamble of claim 1. The invention relates furthermore a method according to the preamble of claim 15.

In many technical applications, process steps occur in which a heat flow is exchanged between two fluids. This heat flow can serve to cool the warmer fluid or to warm up the colder fluid (basic operation of the heat exchange). If reactions take place in one of the existing fluids, the task can be to influence the heat tone of the reaction and the temperature profile in the reactor by integrating heat exchange functions in the same apparatus. For example, the US-A-5,283,050 an integrated reactor that is able to mix or react two or more fluids. The reactor consists of a porous element and a housing having at least two inlets and one outlet.

Such become large-scale industrial Procedures used in various processes, for example for intermediate cooling of exothermic reactors. The heat exchange function is mostly with conventional (fixed bed) tubular reactors spatially from the reactor itself separate: external heat exchanger or heat exchange zones integrated in the reactor are used for intermediate cooling, endothermic high-temperature reactions are carried out in tubular reactors, which are integrated in combustion chambers. The not optimal heat transfer for example in external flame combustion leads to a high volume requirements of process steps as well as large energy flows, which are discharged through the exhaust gas of a described combustion chamber. In the endothermic, catalytic conversion of hydrocarbons with steam to a synthesis gas is, for example, in the conventional reforming reactors only about half of the supplied energy of the fuel gas stream used to apply the enthalpy of reaction. The other half leaves as hot Exhaust the combustion chamber. In large industrial systems the energy content of such heat losses can often still be used.

There has been increased interest in recent years to improve the energy efficiency of refinery processes emerged. This interest has led to the development of various Proceedings conducted, where the energy coupling to carry out endothermic reactions was improved by "heat exchange reformer". The design is similar often that of shell-and-tube heat exchangers.

In parallel with the improvement of Have energy efficiency from continuous processes with very high throughputs fields of application open up, which due to relatively small product quantities and high requirements compactness and energy efficiency. As One example is the implementation of previously unused natural gas reserves ("stranded natural gas ") to high quality Products on site in compact, portable systems. There is a high level of economic motivation behind this application, since 95% of the gas deposits cannot produce as much gas, than that transportation as liquefied gas would be financially interesting. Compact devices should also be mentioned, which are decentralized or mobile use. Potential applications are, for example, in reaction steps in decentralized energy supply systems based on fuel cells in the mobile area with compact Apparatus for auxiliary material production in motor vehicles.

The efficient coupling of heat exchange functions in common devices is large industrial for many State-of-the-art applications, implemented for example using plate heat exchangers. The previously known designs can however for the most part the requirements for inexpensive mass production for many Processes that are industrially relevant but implemented on a small scale not or only in modified Fulfill shape.

The energy-efficient integration of heat exchange and reaction functions is a current field of research and for applications in the range <500 kW independent from the cost issue for many reaction systems have not yet been implemented. This is especially true then when the reactions are heterogeneously catalyzed and one have strong heat. A current field of research is, for example, energy-efficient coupling of several continuous but spatially separated reactions in one device. With the previously known apparatus designs is for various industrially interesting reaction systems are not convincing Realization for the efficient heat integration and the operation in a device is known.

Problems coupling reactions in a device in spatial separate leadership the heat absorbing / emitting Fluid flows similar to one The tubular reactor is created by the fact that the reactions are carried out separately from each other dependent from the kinetics of the respective reaction system and the reactor operating point (Educt concentrations and educt streams). Due to the strong location dependency of the state variables the temperature control a big challenge in integrated reactors.

It is advantageous to conduct fluids in a manner similar to that in a flow tube reactor, with fluid distribution / collection areas directly into the fore direction can be integrated. In this context, reaction systems are preferably considered in which the conversion rate and thus the temperature profile in integrated reactors can be influenced in a targeted manner by means of one or more side feeds in at least one of the reacting fluids. This applies, for example, to reaction systems whose reaction rate in conventional tubular reactors or monolith structures is estimated to be too high in the inlet area, so that the heat effect caused by the reaction is not evenly distributed over the reactor. An example of this are oxidation reactions, in particular total oxidation reactions or selective oxidations.

Realization of side feeds in compact reactors is known. For example, WO 01/54806 discloses a reactor with a reaction zone and plate type heat exchangers, being the heat exchange medium are in operative contact with the reaction zone, and the Heat exchange means from a plurality of one above the other Plates exist in the liquid channels are molded into a predetermined pattern. The fluid channels are aligned so that they are discrete when arranging the panels Heat exchange paths for fluids to disposal put. The method presented there as well as other suggestions however lack of flexibility on since a side feed only at defined points in the reactor through special supply channels and distribution structures for every Side feed possible is. It is also inexpensive Mass production not possible since in the concept presented a flat connection of metal layers using a diffusion welding process carried out becomes. One locally fluid supply / metering of different sizes distributed in two room dimensions The concept presented cannot perform per material layer.

For So-called multifunctional apparatus, which have several process engineering Basic operations such as heat exchange and integrate at least one reaction are not convincing so far Concepts for realizing a local distributed, highly flexible fluid supply in connection with the possibility known for mass production.

The integrated reactor according to the invention has across from the prior art the advantage that the temperature or reaction in Reactor can be influenced better than before. This will an efficient coupling of heat exchangers fluid streams reached.

Advantageous further developments of Invention result from the measures mentioned in the subclaims.

Short description of the drawings

Embodiments of the invention are shown in the drawings and in the description below explained in more detail. It demonstrate

1 schematically shows a plan view of the integrated reactor according to the invention;

2 schematically the planar structure of the rector geometry according to the invention:

3 a cross section through two layers of the reactor according to the invention;

4 schematically an exemplary embodiment of a locally different perforation according to the invention; and

5 schematically the structure of a special embodiment of the reactor according to the invention.

embodiments

In an integrated reactor, the heat exchange at the same time and involves reaction functions between two fluids, it is for targeted reaction management desirable for various applications, the temperature profile in the reactor better than with previously known To be able to influence methods. Under the influence should be described in the following Reactor geometry a metering of a fluid in at least one other Fluid can be understood. Measures are under targeted influence to influence the heat tone at least a fluid flow by targeted metering of at least one other Fluid flow understood. The in the reactor of the invention The fluids used can both fluid as well as gaseous be it can mixtures can also be used.

The invention aims to be efficient Coupling of heat exchangers fluid streams enable in one device. With efficient coupling, a high efficiency of heat transfer is achieved between the spatially separate fluid flows as well as the targeted influencing of the temperature field in the reactor through flexible fluid metering in at least one other Fluid flow understood. In principle, the reactor concept is intended for mass production be suitable. This suitability is understood as the possibility with little Time and material expenditure to produce large quantities with high quality.

In particular, they are to be used in continuously flow-through devices with different material layers in which at least two fluid flows are spatially separated from one another and, if necessary, are divided into channel structures as part of a parallelization of the flow guidance (see below). In the following, the term channel structure simplifies the entirety of the heat-transferring, flow-guiding structures of a material layer. The concrete one Design of the channel geometry within a channel structure can be location-dependent. The channel cross-section is not limited to square and rectangular geometries. The term channel structure is also intended to encompass other conceivable cross-sections which appear to be meaningful in this context for process or manufacturing reasons.

A parallelization of the flow is by distributing at least one of the at least two in the device out Fluids made on a channel group. In the fluid distribution / merging areas a fluid is applied to the channel structures of a channel group distributed. The channel structures of the channel group can be in different material layers be arranged by the symmetrical stacking of individual Material layers result in a defined sequence. A channel group exists thus from the entirety of all channel structures that are the same Lead fluid.

Depending on the ongoing process the individual channels a channel group either have the same geometry or have dependent on distinguish the location on a planar location. different Geometries within a material layer can be considered for optimization the heat distribution, the mass transfer or the fluid cross-section are based in a planar position.

At least in the channel group, in that another fluid can be added runs at least a reaction. In addition to this channel group is at least one more Channel group available, which heat exchange and / or take over reaction functions can. The wall structure of the further channel group can be perceived of reaction functions catalytically coated no. alternative the channel group can also be uncoated and only heat exchange functions perceive. Furthermore, a channel group can also be a catalytic one Contain material that is not directly on the wall structure must be upset. Rather, the catalytically active material be introduced into the channel group, for example in the form of a catalytically coated and three-dimensionally curved film, or in the form of catalyst pellets, or in another form which is a basic body is coated catalytically active and then in the channel structure of the Reactor is introduced. It should be noted that each channel group for themselves can be coated, the catalytic coating can for every Channel group dependent be chosen differently from the reaction to be catalyzed. In addition, the coating can differ locally in the direction of flow of the fluid. Dependent on the barrel length can basically be a There is a variation in the coating quality. It is under the term coating quality understand that the material composition of the applied Layer may vary. This means for example, that the catalyst activity is targeted along the channel length can be varied that channel areas devoid of a catalytic acting layer can remain and / or that parts of the channel circumference are not coated.

For efficient coupling are both a small size of the device for reasons of energy loss and the operability of the device is crucial. Under operability becomes the possibility in particular for the defined commissioning and operation at different educt mass flows in compliance with the specifications for the product streams of the reactor (Modulability) understood.

The device is made up of several Material layers built up planar. The material layers consist of one metallic material or a plastic, they can depend on the application of different thickness. It becomes a fluid guided in a channel structure per material layer. The locations are after Outside sealed fluid-tight. The pressure range of the reactor is out material reasons preferably at less than 50 bar internal pressure relative to the environment. Although generally higher pressures possible, in these cases is however a flat one Sealing of the reactor, for example by flat diffusion welding or -soldering, to provide for the high forces to be able to better absorb between the individual sheet layers.

The reactor according to the invention can in particular are used to couple two reacting fluid flows, for Coupling of a reacting fluid flow with a heat-exchanging fluid flow, taking both streams Educts can be metered in, and for coupling a reacting fluid flow, the one defined below Conditions a feed stream is metered in with a heat-exchanging Process step, e.g. with the coupling of a heat-absorbing fluid flow a fluid stream in which one or more exothermic reactions expire.

The reactor according to the invention improves existing integrated reactor concepts by optimizing the heat tone by metering in at least one fluid into at least one of the reacting process streams, so that the temperature field in the reactor is influenced in the desired manner. The temperature field in the reactor wall material and in the fluid channels in all three room dimensions is referred to as the temperature field. This enables successful process control between spatially separated reaction systems for many applications. Furthermore, the selectivity of different reaction systems is improved by more targeted temperature control. In addition, a high power density of transferred heat output is guaranteed (both for heat exchange applications that require a high power density and for the heating / cooling of reaction systems large enthalpy of reaction).

In addition, the reactor of the invention serve explosive mixtures by metering in a feed stream in a channel structure while ensuring heat exchange properties to form only inside the reactor. Security for technical Syntheses are thus for decentralized or mobile applications with appropriate design of the channel structures increased.

1 shows a plan view of a reactor according to the invention 10 , Its structure and mode of operation is shown below using the example of heat integration for steam reforming of methane. The endothermic reforming reaction with the educts CH ₄ and H ₂ O (reforming gas) is coupled with the exothermic combustion of a fuel gas, which in the present case is a CH ₄ / O ₂ mixture, for example. In a fluid distribution area 11 becomes the reforming gas 13 each on a corresponding channel structure of a different material layer 12 divided as the fuel gas 14 so that reforming gas 13 and fuel gas 14 in channel structures in different levels of the reactor. The planar, layered construction of the reactor from several layers of material 12 going on at different levels 2 and 3 outlined below. Both fluids react in their respective, separate channel structures predominantly heterogeneously catalyzed, i.e. that the reactions take place on the catalytically coated wall surfaces, since plate reactors, particularly in the case of strongly heat-toned wall reactions, utilize the fact that only the heat conduction through the partition wall transfers the heat between the two Channel structures hindered, are used. In principle, however, homogeneous reactions can also take place.

1 shows a direct current flow of the two fluids 13 and 14 , which means that both fluids are on the same side of the reactor, in the present case in the fluid distribution area 11 , are fed. However, countercurrent flow is also possible, in which the one fluid is in the region of the fluid distribution area 11 and the other fluid in the area of one at the fluid distribution area 11 opposite end of the reactor arranged second fluid distribution area is fed. Since it is a top view of the reactor according to the invention, there is only one channel structure consisting of channels arranged parallel to one another 15 visible, in which the reforming gas in the present example 13 is initiated. Which is the second fluid, in this example the fuel gas 14 , leading channel structure is in a parallel to the channel structure 15 arranged below the level, which is indicated by the dashed arrow. To the fluid distribution area 11 the actual reactor area closes 16 on, in the present example the exothermic combustion of the fuel gas 14 he follows. In the present embodiment of the reactor according to the invention is now in this area 16 the channel group in which the exothermic reaction takes place, another educt (fluid) 22 added. This further fluid is preferably one of the reaction partners, in the present case, for example, oxygen. Depending on the requirements selected, another fluid can also be added. The feeder is about perpendicular to the channels 15 arranged transverse channels 17 realized in which the fluid to be metered via a common feed 18 is fed. The cross channels 17 are arranged between the levels in which the reforming gas 13 and the fuel gas 14 be performed. In the present example, the cross channels extend 17 over the entire channel structure 15 and the corresponding channel structures arranged below, the feed 18 is realized outside of this structure. However, it is also possible to feed them together 18 to be arranged within the channel structure itself. To the area 16 a fluid collection area closes 19 in which the two fluid streams are brought together and discharged from the reactor. In the case of countercurrent flow of the two fluids, this area simultaneously represents the fluid distribution area for the first fluid and the fluid collection area for the second fluid. Accordingly, the fluid distribution area for the second fluid is simultaneously the fluid collection area for the first fluid.

2 shows a section along the line AA of the 1 , which is the planar, layered construction of the reactor from several layers of material 12 (in the example shown 2 Locations) clarified. In the present embodiment, the fuel gas 14 in the upper channel structure 20 (Oxidation channel), and the reforming gas 13 in the lower channel structure 21 (Reform channel) led. Both channels can have a different geometry. Between the two channel structures 20 . 21 are the cross channels 17 arranged (in 2 perpendicular to the drawing plane) through which the fluid to be metered is passed. The metering is carried out via a metering structure arranged parallel to the respective channel structures, that is to say perpendicular to the transverse channels 23 , This metering structure is preferably flat, parallel to the material layers 12 running, perforated foils 23 , For metallic devices, this foil can consist of metal, or it can be a thin, appropriately processed metal sheet. Depending on the temperature range of the reactor, the use of plastics, porous ceramics or composite materials is also possible. Of course, combinations of materials, such as metal as the base material and plastic as the material for the foils, are also included. The enlargement of the 2 illustrates this arrangement. Both layers of material 12 . 12a consist, as already mentioned above, of a metallic material or of Plastic or ceramic. It should be noted that both layers of material can also consist of different materials, for example different metal alloys. In addition, the materials can generally be of different sheet thickness and geometry.

In the 2 Upper material layer in which the fuel gas is conducted (oxidation channel) has a smaller cross section in the present embodiment than that under material layer in which the reforming gas is conducted (reforming channel), both layers of material can be sealed fluid-tight to the outside by metal or plastic layers , Sealing by laser welding methods is preferably provided, so that no special sealing material has to be supplied. The educts carried in the corresponding channels, which are fed into the reactor in the fluid distribution area located on the left side of the structure, pass through the transverse channels as they pass through the respective channel structures 17 (arranged perpendicular to the plane of the drawing), from where the fluid to be metered through the perforated film 23 is fed into the oxidation channel, which is indicated by the curved arrows. On the side opposite the fluid distribution area, the products of the oxidation or reforming channel become the fluid collection area ( 8th in 1 ) passed and led out of the reactor there.

3 shows a cross section through two layers of material of the reactor according to the invention along the line BB in 2 , This figure clearly shows the structure of the respective material layers 12 made of a metallic or plastic material 25 and the channels formed in it 20 . 21 recognizable. Furthermore, the 3 can be seen that both layers of material 12 have different geometries. The metering structure is between the two layers of material 23 arranged in the form of a perforated film through which the fluid to be metered in from the transverse channels 17 (in 3 shown in dashed lines, because the respective material layers are covered) is fed into the corresponding channel. Advantageously, as in 3 shown the channels 20 integrated into the material layer that guides the fluid flow into which no metering is carried out (in the present example, the reforming channel).

4 shows schematically an exemplary embodiment of the metering structure in the form of a perforated film 23 , in which 4 a view along the line CC in 3 represents. Size and number of in the slide 23 Perforations containing may vary depending on the position. In this way it is possible to feed the fluid to be metered in at different positions in different concentrations into the corresponding channel structure, as a result of which a desired influence on the fluids guided in this channel structure can be obtained.

The distributed metering is designed in such a way that the heat of the combustion reaction is influenced in the desired manner for at least one operating point of the reactor. For this purpose, the distributed supply of a large part of the required oxygen, which can also be atmospheric oxygen, through the transverse channels is considered here as an example. Ideally, the temperature in the reactor wall material drops shortly before it leaves the reaction area ( 16 in 1 ) does not decrease significantly.

The start-up of the reactor is facilitated by the distributed reaction of a highly inflammable, hydrogen-containing gas stream: For this purpose, in the fluid distribution area ( 11 in 1 ) of the oxidation channel by an electrical ignition source either heats a hydrogen-containing gas stream or generates a hydrogen-containing gas stream, for example by the catalytic decomposition of a hydrocarbon-containing gas with a hot surface. Soot deposited on the hot surface of the ignition source is burned off at the ignition source when a hydrocarbon / oxygen-containing gas mixture is metered in later.

The axial reaction of the hydrogen-containing gas stream can be achieved by the targeted supply of an oxygen-containing oxidizing agent through the transverse channel structure described 17 get supported. The hydrogen-containing gas stream heated by the ignition source is used to raise the temperature at least in some areas of the reactor to such an extent that the combustion reaction of a methane mixture with an oxygen-containing gas stream can then ignite.

The design of the cross-channels used for metering is preferably chosen so that the pressure loss in the cross-channel is significantly lower than that via the metering structure. In this way, targeted fluid metering can be achieved through the metering structure into the channel structure in which the reacting medium is conducted. The pressure loss in the cross channel or in the metering channel (the metering structure does not necessarily have to consist of cross channels) is compared with the pressure loss due to the metering structure, for example the film 23 , kept very low in that the channel cross-section in the channel structure 17 In accordance with the known rules of technology, the free cross-section of the perforated film or the metering structure is chosen to be significantly larger.

At the same time or alternatively, the supply of the feed stream to be metered in can be selected such that the fluid to be metered in changes along the channel. This is ensured by the fact that the fluid supply and distribution to the transverse channels is subdivided into several areas, each of which is supplied with other fluids for metering. Each of the areas receives its own supply of the fluid to be metered in ( 18 in 1 ). Just as with the metering of a single fluid, it is possible to cross the channels of a metering structure already in the channel structure. In this way, the fluid distribution in each metering structure is significantly simplified in terms of construction.

Another application of the reactor according to the invention lies in the coupling of two reacting fluid flows, the a further educt mixture is metered in each case. This will follow on Example of coupling the reaction enthalpy of an exothermic reacting gas flow to heat / ensure the phase transition of a second fluid closer explained.

In polymer electrolyte membrane fuel cells can be supplied on the anode side Hydrogen not complete be implemented. The hydrogen-containing anode exhaust gas flow must Derivation into the environment from energetic and safety-related establish be free of hydrogen and methane. A frequently pursued concept for Anode exhaust gas utilization is the catalytic conversion of the anode exhaust gas. Ignites due to the hydrogen content the reaction even at low temperatures. Because of the coupling a strongly exothermic reaction with the strongly endothermic evaporation process with conventional evaporators a challenge in the uniform heat input and distribution.

In the sense of the reactor according to the invention, the hydrogen-containing gas stream can be supplied distributed over the transverse channels, and the oxidizing agent is metered in at the beginning of the channel. Alternatively, it is conceivable that the oxidizing agent is metered in via the transverse channels and the hydrogen-containing anode exhaust gas is metered in via the fluid distribution area 18 is dosed into the channel. Through a suitable distribution of the perforation, a complete conversion of the hydrogen / hydrocarbons in the channel can be achieved.

By appropriate temperature control and The reactor according to the invention can select materials in addition to evaporation also overheating tasks of the gas-steam mixture produced. This concept is particularly useful for carrier gas evaporation from low Suitable hydrocarbons, the evaporator as to be evaporated The starting material is a mixture of hydrocarbon and liquid, usually water. To reduce uneven evaporation a realization is conceivable in which the one to be evaporated liquid fed at the beginning of a channel and then this with the hydrocarbon dosed through a separate perforation while the evaporation is mixed.

The described addition of two different fluids into a channel structure is shown in 5 shown. The variant is based on the fact that two auxiliaries are metered into different streams through perforated foils. The evaporation carrier gas is distributed to the channel structure 27 supplied, ie that the carrier gas of the evaporation is metered along the channel, the metering thus takes over a mixing function. A hydrogen and / or hydrocarbon-containing fuel gas is used in the second channel structure to heat the evaporator 28 as described above via cross channels 17 (in 5 dotted). The simple symmetrical expandability through the parallelization of the flow in the reactor according to the invention is illustrated by the representation of further metering structures 26 . 29 which are the channel structures 27 and 28 include, shown.

Another example of a use of the proposed reactor lies in the selective CO oxidation to CO ₂ for the operation of polymer electrolyte membrane fuel cells with a hydrogen-containing gas stream which is generated from hydrocarbons. In addition to high catalyst activity and selectivity, the process control is crucial for high CO conversion and high selectivity with little outflow of the side reaction H ₂ + 0.5 O ₂ H ₂ O. Process control here specifically refers to the supply of the oxidizing agent as defined as possible and the most exact temperature control possible , A minimum temperature is necessary to enable CO oxidation, while a maximum temperature that is around 20 ° C higher should not be exceeded in order to avoid the undesirable accompanying reaction of hydrogen oxidation.

Conventional procedures on a small scale Performance range, which is currently particularly for fuel cell applications are developed, use monolith structures to carry out the reaction. there the reaction step is usually carried out in two separate reactors, between an intermediate cooling step is arranged. An oxygen-containing gas is metered doing so in front of the respective reactor, sometimes an oxygen-containing one Total gas flow in front of the individual reactors even regulated individually.

The even distribution of the oxygenated Gas flow on the monolith structure is only complex releasable Challenge. In addition, safe process control is through the formation of locally explosive mixtures at the mixing point in certain circumstances not given. The temperature control in the selective oxidation in their previous implementation for decentralized Prototype systems have several disadvantages. On the one hand there is the apparatus Relatively high effort, since two reaction stages and a heat exchange function thermally largely without integration. Second, exist independently from the constructive. Effort Disadvantages in inaccurate temperature control. episode can catalyst damage by overheating, inadequate sales rates, lack of selectivity of the process and in extreme cases a "runaway" response due to the spatially separate reaction and heat exchange areas his.

The integration of an efficient heat rope The defined, distributed metering of the oxidizing agent in accordance with the reactor proposed here promises great advantages with regard to uniform temperature control and high conversion rates. In this application, the fluid stream into which the oxygen-containing gas stream is metered through the transverse channels is the hydrogen-containing gas-steam mixture from the reforming process.

The security of the process will clearly increased, if sufficiently small structures are chosen that appropriate design ensure good heat dissipation. In addition, the risk of explosion is largely prevented, since when used of the reactor concept presented, the mixture between oxidizing agent and the hydrogen-containing reformate stream takes place in the reactor itself. Mixtures with explosive Concentrations are only formed within the apparatus. explosions are not to be expected with an appropriate design, as a high heat transfer there are limits to the wall material of the heating.

If necessary, in addition to distributed educt metering the heat dissipation selective oxidation by at least one further channel structure respectively. This structure preferably has only a heat exchange function is therefore not catalytically coated. For the same or similar applications can however also provide a catalytic coating be in which one or more endothermic reactions can take place.

Yet another example of using the reactor according to the invention lies in the combustion of a hydrogen-containing synthesis gas mixture to provide energy for an endothermic reaction that takes place in the further channel structure. there becomes hydrogen-containing in one of the two channel structures Gas mixture burned. The oxidizing agent is distributed to a even release the heat of reaction to reach. Due to the distributed addition of the oxidizing agent two problems are avoided. For one thing, education is becoming more explosive Prevents mixtures from entering the reactor because of mixture formation only takes place inside the reactor, on the other hand the heat release with appropriate design evenly distributed over the length of the reactor. This eliminates the well-known problem of high excess temperatures in the entrance area of a catalytic area in extremely fast reactions such as significantly reduced hydrogen oxidation.

The reactor according to the invention creates the possibility heavily heat consuming with heat emitting Process steps in a device efficiently by increasing the Degrees of freedom by means of targeted fluid metering into a channel structure to couple. The more targeted fluid metering than in previously known Devices a support for defined temperature control in compact apparatus in which at least one reaction takes place. Based on the advantages regarding The reactor according to the invention permits flexible metering of a feed stream for the first time mixing explosive media directly at the reaction site with simultaneous integration with heat exchange functions.

For numerous applications have advantages over devices in which energy coupling, for example through external combustion reactions takes place and devices in which none or only one or more local additions of a starting material to a fluid stream are realized is. Across from the latter are particularly advantageous in terms of their location flexible and easy to implement design of the Dosing.

Further advantages of the invention are subdivided in those that involve the integration of several process steps in one Device generally connected, as well as those that. specially with the proposed implementation of the distributed educt metering are connected. It can be assumed that according to the current one State of the art the first-mentioned advantages of the reactor according to the invention for many Reaction systems at all can only be used.

Benefits with integration several process steps are connected in one device For example, the better use of the reaction enthalpy of an exothermic Reaction system for heating an overall endothermic reaction system. This reduces the efficiency of heat recovery following the fluid distribution / merging areas of the energetically not optimally usable enthalpy flow of waste heat.

Another advantage is that compact implementation of the process function by integrating several Part process steps. In addition to the low space requirement, which with a Design of the duct structure to optimize heat and Mass transfer operations goes hand in hand with known rules of technology the advantage of reducing heat loss through increased compactness the device. While for large industrialists Processes due to the large material flows often with sufficient accuracy from adiabatic behavior the device can be assumed to be the case with the ones described here Fields of application frequently not the case. The concept presented also enables the subdivision in principle the cross channel feeds in individual sections in the channel direction.

Advantages that are specifically associated with the proposed implementation of the distributed educt metering are, for example, in the low construction effort for realizing a two-dimensionally distributed educt metering, and in greater freedom in the amount of the added volume menstromes through different diameters of the perforation of the dosing structure.

There is also an advantage by improving the mode of operation, because at commissioning the device can be heated with great uniformity. Through the cross channels can, for example, a starting material mixture evenly on the reaction area be distributed, which catalytically with a second educt, the flows through the channel structure, releasing heat reacted. The mode of operation may well be during the start-up phase to be discontinuous.

Advantages continue to arise through the avoidance of strong temperature gradients in the reactor Starting operation. High temperature gradients can become undesirable Tensions. in the active ingredient, in particular, however, to flake off catalyst layers to lead. Microreactors as a special case of compact reactors are for safe Litigation also potentially explosive gas components due to their good heat transfer properties known. Through the implementation of a distributed described here Educt metering is the potential of compact reactors compared to known ones Realizations further increased, because the newly created possibility of a defined and distributed merging of two Educts controlled by metering in an educt in a reaction channel at the site of the reaction open up new perspectives in process design. It also follows an easy scalability of the integrated device through the Parallelization of the flow guidance (a Channel group consists of a requirement-dependent number of channel structures).

The reactor geometry presented offers with the possibility distributed educt admixture, for example, also advantages if in the chosen one Temperature range very rapid reactions are carried out, because the reaction zone is more uniform than locally with previously known methods can be distributed in two dimensions.

Claims (19)

Integrated reactor ( 10 ) with at least two spatially separated channel structures ( 20 . 21 ) for guiding at least two fluid flows, with at least one fluid flow within a reaction area ( 16 ) a reaction takes place which produces a heat tone, and at the same time heat transfer takes place between the fluid flows, characterized in that at least one of the at least two fluid flows over the entire reaction area ( 16 ) at least one further fluid can be metered in distributed. Integrated reactor according to claim 1, characterized in that the reactor ( 10 ) from a plurality of layers of material arranged in parallel ( 12 ) consists. Integrated reactor according to claim 1 or 2, characterized in that the fluid to be metered in via transverse channels arranged perpendicular to the direction of flow of the fluid streams ( 17 ) is feasible. Integrated reactor according to claim 3, characterized in that the transverse channels ( 17 ) in the material layer ( 12 ) are integrated, in which the fluid flow is guided, into which no further fluid is added. Integrated reactor according to claim 1 or 2, characterized in that the. The at least one further fluid is metered into the corresponding channel structure via a metering structure ( 23 ) can be realized. Integrated reactor according to claim 5, characterized in that the metering structure ( 23 ) flat and parallel to the material layers ( 12 ) is arranged. Integrated reactor according to claim 5 or 6, characterized in that the metering structure ( 23 ) is a film with perforations. Integrated reactor according to claim 7, characterized in that the foil is made of a metallic material or plastic consists. Integrated reactor according to claim 7 or 8, characterized characterized that the size and the Number of perforations depending from their local position is variable on the slide. Integrated reactor according to claim 5 or 6, characterized in that the metering structure ( 23 ) is a porous ceramic structure. Integrated reactor according to one of claims 3 to 10, characterized in that the pressure loss in the transverse channels ( 17 ) is lower than that above the dosing structure ( 23 ). Integrated reactor according to one of the preceding claims, characterized in that the fluid to be metered in along the reaction region ( 16 ) is variable. Integrated reactor according to claim 12, characterized in that the supply of the fluid to be metered into several areas along the reaction area ( 16 ) is divisible. Integrated reactor according to one of the preceding claims, characterized in that at least one channel structure ( 20 . 21 ) has a catalytic coating. Integrated reactor according to one of the preceding Expectations, characterized in that the separate channel structures have different geometries. Process for targeted reaction control in one Integrated reactor with at least two spatially separated Channel structures for guidance at least two fluid flows, wherein in at least one fluid stream within a reaction area a reaction takes place that causes a warming effect, and at the same time a heat transfer between the fluid flows takes place, characterized in that at least one of the at least two fluid flows over the at least one additional fluid is distributed throughout the reaction area is metered. A method according to claim 16, characterized in that the fluid to be added is vertical to the direction of flow the fluid flows arranged transverse channels guided and the at least one fluid flow over a flat, with perforations provided dosing structure is metered. Use of the integrated reactor after one of claims 1 to 15 for energy efficient evaporation and overheating for mobile and stationary Fuel cell system. Use of the integrated reactor after one of claims 1 to 15 for selective carbon monoxide oxidation in fuel cell systems.