DE19953233A1 - Autothermal reactor circuits for the direct coupling of endothermic and exothermic reactions - Google Patents

Abstract

A reactor circuit for autothermic coupling of exothermic and endothermic reactions with separate conduction of both reaction flows, comprising heat exchanging sections (2, 9, 19) between all supplied educt gases (1, 4, 8) and all hot product gases (3, 10), in addition to a reaction area (7, 11, 12) wherein exothermic and endothermic reactions occur in a direct exchange of heat, said exchange occurring in the heat exchanging sections (2, 9, 19) between the supplied educt gases (1, 4, 8) and the hot product gases (3, 10, 15) either in a recuperative manner in a counter flow or in a cross-counter flow or in a regenerative manner, the heat capacity of one partial flow in each heat exchanger section corresponding approximately to the heat capacity of the other partial flow, the exothermic and endothermic reaction in one reaction area (7) respectively occurring in a chronologically or spatially separate manner, whereby the two partial areas (11, 12) in the case of a spatial separation are locally coupled to each other in such a way as to result in an excellent exchange of heat therebetween and whereby the exothermic reaction in the case of a spatial and chronological separation is influenced in such a way that it only begins upon arrival in the reaction area thereof (11) and the reaction heat is released in a substantially evenly distributed manner over a relatively large local area which overlaps with the reaction area of the endothermic reaction (12) and is transferred to the endothermic reaction.

Description

The invention relates to methods for the direct coupling of an endothermic synthesis reaction with an exothermic accompanying reaction. Endothermic synthesis reactions play an important role in the production of soil in the chemical industry chemicals and intermediates. These reactions are mostly in the gas phase at elevated temperature and often on solid catalysts in a so-called fixed bed reactors carried out. Typical examples are coal reforming reactions Hydrogen for the production of synthesis gas and dehydration.

The required heat of reaction is achieved through an exothermic accompanying reaction, typically a combustion reaction, generated and mostly by indirect Transfer heat exchange to the reaction gas. The heat is transferred Carried in upstream or intermediate heat exchangers, in tube bundle cracks gates, which are surrounded by a hot heat transfer fluid, or by using Catalyst-filled reaction tubes are arranged directly in a combustion chamber. In these arrangements, the heat input takes place relatively untargeted, so locally high excess temperatures occur and the product gas relatively long at high temperatures temperatures remain, which favors undesirable secondary and subsequent reactions. Au In addition, the heat contained in the hot exhaust gases can only be increased wall (expensive high temperature resistant heat exchanger) and at moderate tempe recover the level of the building and only continue in a suitable energy network use.

Therefore, there were numerous considerations and attempts to get the required response generate heat directly in the reaction system and in the sense of an integrated reak tion management to be used there to such an extent that the inflows and outflows hend "cold" and no excess heat must be dissipated. Such Reaction control is referred to below as "autothermal", with "cold" the  Corresponds to temperature at which the feed materials z. B. after an evaporator or Compressor are present, and the heat contained in the discharge streams no longer is economically usable.

The basis for a suitable autothermal reaction is the best possible energetic coupling of an exothermic accompanying reaction with the desired endo thermal synthesis reaction. A direct regenerative is expediently or an indirect recuperative heat exchange between the hot reactor run and the cold reactor feed proposed. The previously proposed Kon Scepters, however, consistently show difficulties, so that no large-scale techni realizations have become known.

[1] describes a process for steam reforming methane in a reactor periodic flow reversal presented. The reaction mixture is so much oxygen added to make the overall reaction exothermic. By the brisk Native heat exchange in the reactor will lead to an autothermal reaction aims. The experiments show very narrow and high temperature peaks with the Ge drive from catalyst damage, a very high parametric sensitivity and Problems of back reaction and coke formation in the falling part of the tempera door profile.

[2, 3] also describes the behavior of a reactor with a periodic flow for methane steam reforming. In contrast to [1], the Heat of reaction for the endothermic reforming reaction is not simultaneous to this provided. Rather, the reforming gas mixture is during a half period from one side of the reactor, a fuel gas mixture during the second half period fed from the other side. The authors show that stable operation only in a very narrow operating range and with unsatisfactory behavior is possible. Again, very steep, high temperature peaks are characteristic during the fuel gas phase. It can in the narrow high temperature zones not enough heat is stored for the subsequent endothermic period the. In [4] it is shown that an inert Improvement but no overall satisfactory behavior can be achieved. In [5] the methane steam reforming is used instead of regenerative with recuperative Heat exchange in a so-called "countercurrent fixed bed reactor" examined. the authors show that by appropriate choice of the catalytically active and the inert areas achieved an improvement in the originally unsatisfactory reactor behavior  can be. The disadvantages, however, remain a very narrow, steep reaction zone and an overall unsatisfactory heat integration, since the combustion reaction one already starts thermally shortly after the inlet, so that on the fuel gas a sufficiently long heat exchange cannot be realized.

In [6, 7] an autothermal reaction with periodi proposed change of flow direction in which the reaction heat me is achieved via a hot gas stream fed into the middle of the reactor. Here too the heat integration turns out to be not completely satisfactory because of the bulk tion area, which is flowed through by reaction gas and hot gas, a higher Throughput has as the part that only the reaction gas flows through.

Overall, all of the previously known concepts for the autothermal coupling of exothermic and endothermic reactions have serious disadvantages, which can be summarized in the following points:

• - very high, narrow temperature peaks, caused by local or time separation of the exothermic and endothermic reaction zones,
• - uncontrolled (homogeneous) start of the combustion reaction,
• - poor heat integration, d. H. Partial streams leave the reaction system tem too hot.

Task and problem solving

The task thus arises of new reactor configurations for the autothermal Coupling of an endothermic synthesis reaction with exothermic accompanying reactions develop that does not have the above disadvantages or only to a significantly reduced extent have. This task is accomplished by the one set out in the claims Developments according to the invention solved.

The basis of the problem solution according to the invention is on the one hand ensuring one optimal heat exchange between hot outlet and cold inlet. A sol As is well known, optimal heat exchange can only take place via an indirect counter electricity heat exchange or a sufficiently fast direct regenerative Heat exchange takes place if the in both directions per time unit / removed material flows have the same heat capacity. A first characteristic Cum of the problem solution according to the invention is that in the heat exchanged material flows each have the same heat capacity. Since the  Heat capacity changes due to temperature change and chemical reaction in practice, this requirement can only be met with a certain bandwidth. The second requirement is that steep, high temperature peaks are avoided have to. As the examples discussed above show, this tempera comes peaks always occur because the exothermic accompanying reaction very quickly, happens almost spontaneously and spatially separated from the endothermic reaction. In particular especially when the exothermic and endothermic reaction is carried out in countercurrent there is a pronounced tendency of the two reaction zones to differ from one another to separate locally. The higher the reaction rate, the greater the tendency are speeds of the two partial flows. The second character according to the invention Teristikum thus says that the two partial reactions are so damped and their react tion zones must be extended so that their overlap area as possible gets big. Suitable measures for this are a restriction of the catalytically active tive areas to a common overlap zone and the damping of the kata lytic activity by catalyst dilution or a suitable rapid Auf sequence of catalytically active and inactive sections. Particularly advantageous is also a change from countercurrent to direct current in the ge common reaction zone or the implementation of the exothermic reaction largely mixed conditions, e.g. B. in a fluidized bed. Where not? is possible, the heat released in the exothermic reaction must be very ef fective transport mechanisms in the area of the main reaction zone of endo thermal reaction can be transported.

The third requirement is that the heat of the exothermic accompanying reaction only in the Area of the desired (catalytically active) reaction zone of the endothermic syn thesis reaction and there (requirement 2) as controlled as possible and distributed locally may be set. As shown in [5], this cannot always be done by an equivalent Reach appropriate arrangement of the oxidation catalyst. An inventive Procedure says that z. B. only a reactant of the exothermic reaction on desired reaction site is mixed. It can be in the sense of the two ten demand prove to be expedient, the interference on several over the ge desired discrete or continuously distributed feed locations columns.  

Examples

In the following examples according to the invention, lessons are given, such as the three of the above requirements can be met at the same time.

Fig. 1a shows a basic form of the embodiment according to the invention in the event that the flows of the endothermic synthesis reaction and the exothermic Begleitreak tion must be performed separately, ie must not be mixed ("separate reaction management"). The reaction medium of the exothermic reaction 1 is fed into the reaction space 7 via a heat exchanger 2 . The exhaust gas from the exothermic reaction 3 leaves the reaction chamber 7 and gives off its heat in the heat exchanger 2 to the inlet 1 . For reasons of energy efficiency, the heat exchanger 2 will expediently be a countercurrent or cross-countercurrent heat exchanger. Alternatively, regenerative heat exchangers in a clocked single or multiple bed or rotor arrangement are also suitable. In a comparable manner, the reaction mixture of the endothermic reaction 8 is fed to the reaction chamber 7 via a heat exchanger 9 and the product mixture 10 formed is discharged through the heat exchanger 9 .

If there is a risk that the reaction mixture for the exothermic reaction 1 already reacts in the heat exchanger 2 , a reactant 4 (expediently the deficit component) must be fed to this reaction separately and only added immediately before or in the reaction space 7 (feed 5 ). To achieve a uniform heat transfer in the reaction chamber 7 , it may be expedient to feed the deficit component additionally at several points 6 locally or locally into the reaction chamber. If the reactant 4 represents only a small heat capacity flow compared to the other reactants 1 , it can be fed directly to the reaction space 7 without thermal coupling with the heat exchanger 2 . Otherwise, it should be heated in the heat exchanger 2 as indicated in FIG. 1a. A corresponding division of the supplied reactants can also take place for the side of the endothermic reaction if a pre-reaction in the heat exchanger 8 is to be excluded.

The reaction space 7 is divided into an area 11 for the exothermic reaction and an area 12 for the endothermic reaction, both areas being in intensive heat exchange. The aim of the design of the reaction chamber 7 is to locally transfer the heat released by the exothermic reaction as completely and uniformly as possible to the endothermic reaction, so that strong temperature fluctuations in the reaction chamber 7 are avoided. One measure according to the invention for this is the direct current flow of current 1 and current 8 , as shown in Fig. 1a. The initial reaction rate of the endothermic reaction at the entry into the reaction space 12 should be chosen so that the heat demand rate of the endothermic reaction corresponds to the heat production rate of the exothermic reaction. This requirement can be achieved by setting the catalyst activity for the endothermic or exothermic reaction and / or by selecting the inlet temperatures in reaction chamber 11 or 12 , ie by designing the heat exchanger 2 or 9 . Another measure is the previously mentioned locally distributed replenishment of the reactants 4 by means of the feeds 6 . This distributed replenishment is particularly expedient if, for apparatus reasons, a countercurrent flow 1 and 8 was selected. In this case, it may be appropriate to the catalyst activity of the endothermic reaction z. B. by dilution or a rapid succession of active and inert sections so far that the endothermic reaction extends over most of the reaction space 12 .

Another measure according to the invention is to ensure a high heat transfer parallel to the direction of the streams 1 , 8 in the reaction chamber 7 . This can be done by thermally conductive internals, by heat pipes or by a meandering or spiral flow of both reaction streams 1 , 8 in the reaction chamber 7 . Alternatively, an extra heat transfer circuit can be arranged in the reaction space 7 .

Another measure according to the invention is to carry out one of the two reactions, but preferably the exothermic reaction, in the reaction space 7 in a fluidized bed, the reaction channels for the endothermic reaction being immersed in this fluidized bed and absorbing the heat of reaction as directly as possible.

In a concretization of the above basic concept for a steam reforming of hydrocarbons, the reaction mixture 1 z. B. consist of air. Part of the feed hydrocarbons or another fuel-rich (waste) gas is mixed in at the feeds 5 , 6 as the reactant 4 . The combustion reaction takes place on the fuel gas side 11 of the reaction chamber 7, depending on the temperature required, on an oxidation catalyst or homogeneously and expediently on a porous support structure. On the reforming gas side, a mixture of hydrocarbon gas or steam and water vapor in the heat exchanger 9 is heated in countercurrent to the hot discharge and supplied to the reforming gas side 12 of the reaction chamber 7 . Steam reforming takes place there on a suitable catalyst, the catalyst being arranged as close as possible or directly to the heat exchange surfaces for the combustion reaction. The temperature profiles to be expected in the individual sections of the basic concept according to FIG. 1a are indicated schematically in FIG. 1b. As a result of the approximately equal heat capacity flows in the counterflow heat exchangers 2 , 9 , the temperature profiles in the heat exchangers are largely straight and parallel. Due to the direct current heat exchange and the side feed of fuel gas, the profiles shown in reaction chamber 7 result approximately. They can be further smoothed if the above-mentioned requirement for equal starting rates for heat consumption and heat production is better met and / or the axial heat transport is improved by the measures mentioned. In principle, similar temperature profiles result if, instead of the counterflow (or cross / counterflow) heat exchangers assumed here, regenerative heat exchangers in the form of clocked or rotating fixed beds are used. In all the cases discussed, it may be appropriate to equip the outflow part 10 of the heat exchanger 9 with shift catalysts if a hydrogen-rich (low-CO) product gas is required.

Fig. 2a shows a basic form of the invention for the case that the exothermic and the endothermic reaction takes place in the same reaction mixture ("simultaneous reaction management"). The reaction mixture 13 is heated in countercurrent to the product mixture 15 in the heat exchanger 14 and then enters the reaction space 16 . If there is a risk that a pre-reaction occurs in the heat exchanger 14 , a selected reactant 4 must be fed in again separately and either metered in completely at the feed 5 or distributed over the reaction space 16 . The reaction chamber 16 is designed so that a strong additional heat transfer takes place parallel to the main flow direction, so that the heat released during the exothermic reaction can be coupled as completely as possible and without excess temperature development into the endothermic reaction. Measures according to the invention for this are highly heat-conducting internals, heat pipes or a meandering or spiral flow guide. If an undesirable byproduct formation does not speak against it, it also makes sense to design the reaction chamber 16 as a fluidized bed, into which the inlets 5 , 6 , 13 are injected and very well distributed and mixed.

In a specific embodiment of the basic concept of FIG. 2a for the oxidative steam reforming of hydrocarbons, the hydrocarbon / water vapor mixture is supplied as stream 13 and oxygen or air as stream 4 . The re action space 16 can be designed as a fluidized bed reactor with the catalysts for the oxidation and the reforming reaction as a fluidized bed. Alternatively, a solid catalyst, e.g. B. in monolith form, through which circulates an inert, ab abrasion-resistant eddy. At correspondingly high temperatures, the catalyst in the reaction chamber 16 can also be dispensed with entirely if the homogeneous reactions are sufficiently rapid. Then it makes sense to provide 14 catalysts for post-reforming or the water gas shift reaction in the outflow part of the heat exchanger.

The expected temperature profiles of the basic concept of FIG. 2a are given schematically in FIG. 2b. For a countercurrent heat exchange in FIG. 14, approximately straight and parallel profiles again result. In the reaction chamber 16 , the overshoot of the temperature caused by the preferential starting of the exothermic combustion reaction is less, the better the additional heat transport was realized parallel to the main flow direction.

Fig. 3a shows a special case of the separate reaction when the heat capacity of the fluid stream 1 , 3 for the exothermic reaction and that of the fluid stream 8 , 10 for the endothermic reaction is approximately the same. Then, instead of the arrangement according to FIG. 1a with separate heat exchangers 2 , 9 , an arrangement with a common counterflow heat exchanger can also be selected, in which the reaction space 7 is also integrated. In contrast to already known similar countercurrent arrangements [5], an embodiment according to the invention according to FIG. 3a must meet the conditions that the heat capacity flows 1 , 3 and 8 , 10 are similar, ie do not differ by more than a factor of 2 and are on - or multiple feeding of the reactant 4 into subspace 11 of the reaction zone 7 takes place. With regard to the appropriate choice of the catalyst activity of the endothermic reaction, what has been said in the discussion of FIG. 1 applies. It is also expedient that the axial heat transfer in the region of the reaction zone 7 is significantly increased by heat-conducting internals or heat pipes 17 . A change of the flow guidance so that the heat-exchanging reaction sections 11 and 12 are flowed through in direct current corresponds to a procedure according to the invention. The temperature profiles to be expected for the same heat capacity flows are outlined in FIG. 3b.

In comparison to the basic form of the separate reaction according to FIG. 1a, the requirement for almost identical heat capacity flows for the exo therme ( 1 , 3 ) and the endothermic reaction ( 8 , 10 ) applies to FIG. 3a. Only then will there be an efficient heat exchange and a minimal need for reactants for the exothermic accompanying reaction. In contrast, the heat capacity flow of the exothermic Begleitreak tion according to Fig. 1a can be chosen freely. The required heat exchange surface of the heat exchanger 2 must then be adjusted accordingly. It must be emphasized that the total heat exchange surface requirement for the same heat recovery is similar for both configurations. However, the embodiment can according to Fig. 3a easier to achieve in a single apparatus.

Fig. 4a shows an embodiment in which the heat supply for the endothermic Re action takes place in that the reaction chamber 12 is mixed with a hot burner gas 5 , 6 . This burner gas is generated by the combustion of two partial flows 1 , 4 in a combustion chamber 18 . These two partial flows are preheated in the heat exchange with a drain flow 3 in the heat exchanger 2 . The reaction mixture of the endothermic reaction 8 is preheated as in Fig. 1a by the hot outlet 10 from the reaction chamber. In contrast to Fig. 1a, the reaction space now consists only of the sub-space 12 for the endothermic reaction, in which the hot fuel gas is mixed as a heat carrier at points 5 and 6 . A partial flow 3 of the outlet of the reaction chamber 12 is performed over the fuel gas heat shear 2 . This partial flow should be so large that its heat capacity in et wa corresponds to the heat capacity of the two partial flows 1 and 4 . Then follows in the heat exchanger 2 an energetically optimal heat recovery with temperature profiles according to Fig. 4b. The local temperature fluctuations in the reaction space 12 can again be minimized by generating additional heat flows parallel to the main flow direction of flow 8 . Here, too, a fluidized bed reactor offers itself similarly as in FIG. 2a for the reaction chamber 16 , the streams 8 , 5 , 6 being fed into the fluidized bed and being distributed through it.

An arrangement according to FIG. 4a is particularly suitable for carrying out dehydrogenation reactions such as styrene synthesis by means of ethylbenzene dehydrogenation. The hot burner exhaust gas 5 , 6 is expediently generated by stoichiometric combustion of the dehydrogenation exhaust gas. It then preferably contains water vapor, which counteracts coking of the catalyst, and inert gas, which together with the water vapor lowers the reactant partial pressure and thus has a favorable effect on the equilibrium of the volume-increasing reaction.

Instead of the recuperative heat exchanger 9 in Fig. 4a, two regenerative heat exchangers 19 can be inserted with periodic changes in the flow direction. Fig. 5 shows a corresponding configuration. The supply lines 1 , 4 for the combustion chamber 18 are expediently integrated into the regenerative heat exchanger 19 . The reaction chamber 12 is now flowed through together with the two regenerative heat exchangers 19 in a periodic alternation from left to right and from right to left. The burner exhaust gas is continuously blown into the reaction space 12 and distributed. The temperature profiles then largely correspond on average to those of FIG. 4b.

A structure according to FIG. 5 can also be used for the simultaneous reaction control according to FIG. 2a if, instead of the recuperative heat exchanger shown there, generators are used. In Fig. 5 then only the burner 18 is omitted. The reactant 1 or 4 (in an oxidative reforming air or oxygen) is preheated via the supply lines running in the regenerators 19 and introduced and distributed at the positions 6 in the reaction chamber 12 . It makes sense for energetic reasons to switch the feed direction of the reactants 1 and 4 with the change of the flow direction, so that the heat capacity flows are approximately the same for both flow directions.

The meandering or spiral configuration of the reaction chamber, which is mentioned in connection with the improvement of the heat transport parallel to the main flow direction, is exemplary and highly schematic in FIG. 6a. The embodiment according to Fig. 6b or 6c would z. B. for the ge in Fig. 1a showed reaction chamber 7 in question. The multiple winding flow path results in a more uniform temperature distribution and heat transfer. The same applies to the design of the reaction chamber 16 from FIG. 2a according to the schematic structure of FIG. 6a.

The examples discussed above show that in the auto-thermal coupling of endothermic and exothermic reactions according to the invention there is a large scope for design. In particular, the heat exchangers shown can optionally be implemented as recuperative countercurrent or cross-countercurrent heat exchangers in tube bundle or plate stack construction, or as regenerative heat exchangers in the form of beds with periodic changes in flow direction or as rotor regenerators (Ljungström heat exchangers). Characteristic of all heat exchanger configurations is that an exothermic pre-reaction, e.g. B. must be prevented by separate management of the reactants 1 , 4 safely. In contrast, it may be appropriate to integrate catalysts for a post-reaction after the endothermic reaction in the reaction space 7 , 12 or 16 in the outflow part of the heat exchanger 9 , 14 or 19 . The reaction space 7 is characterized according to the invention in that the heat of reaction of the exothermic reaction is distributed as uniformly as possible over the length of the reaction space. This can be supported according to the invention in that a reaction component 4 for the exothermic reaction or a hot partial stream is metered in locally distributed, that a direct current or a meandering (or spiral) flow is provided between the fluid of the exothermic and the fluid of the endothermic reaction, that internals with strong heat transfer are provided parallel to the main flow direction or that a circulating auxiliary medium (e.g. in the form of a fluidized bed) ensures such heat transfer. Furthermore, care should be taken to ensure that the heat demand rates of the endothermic reaction and the heat production rates of the exothermic reaction approximately correspond when entering the reaction space 7 . This can be achieved by setting the inlet temperatures (ie designing the respective heat exchanger 2 , 9 ) and / or selecting or influencing the catalyst activity.

literature

[1] RF Blanks, TS Wittrig and DA Peterson. Bidirectional adiabatic synthesis gas generator. Chem. Eng. Sci., 45: 2407-2413, 1990.
[2] MS Kulkarni and MP Dudukovic. Bidirectional Fixed Bed Reactors for Coupling of Exothermic and Endothermic Reactions. AIChE J., 42 (10): 2897-2910, 1996.
[3] MS Kulkarni and MP Dudukovic. Periodic Operation of Asymmetric Bidi rectional Fixed-Bed Reactors with Temperature Limitations. Ind. Eng. Chem. Res., 37: 770-781, 1998.
[4] G. Kolios. For the autothermal control of styrene synthesis with periodic change of flow direction. No. 501 VDI progress reports, series 3.VDI publishing house, Düsseldorf, 1997.
[5] J. Frauhammer, G. Eigenberger, L. v. Hippel and D. Arntz. A New Reactor Concept for Endothermic High Temperature Reactions. Chem. Eng. Sci., 54 (15/16): 3661-3670, 1999.
[6] J. Snyder and B. Subramaniam. A Novel Reverse Flow Strategy for Ethyl Benzene Dehydrogenation in a Packed-Bed Reactor. Chem. Eng. Sci., 49 (24B): 5585-5601, 1994.
[7] G. Kolios and G. Eigenberger. Styrene Synthesis in a Reverse-flow Reactor. Chem. Eng. Sci., 54 (15/17)): 2637-2646, 1999.

Label list

1

Reaction mixture (starting materials) of the exothermic reaction

2nd

Heat exchanger for the inflow / outflow of the exothermic reaction

3rd

Reaction process (products) of the exothermic reaction

4th

a selected reactant (educt), without which the exothermic reaction does not take place

5

Reactant entry point

4th

at the entrance to the reaction space

7

6

Intermediate feed point for reactant

4th

7

Reaction space, separated into areas for the exothermic (

11

) and the endo thermal reaction (

12th

)

8th

Reaction mixture (starting materials) for the endothermic reaction

9

Heat exchanger for the inflow / outflow of the endothermic reaction

10th

Reaction process (products) of the endothermic reaction

11

Part of the exothermic reaction of

7

12th

(Partial) space of the endothermic reaction

13

Reaction mixture (starting materials) of the simultaneous reaction

14

Heat exchanger for the inflow / outflow of the simultaneous reaction

15

Reaction process (products) of the simultaneous reaction

16

Reaction space for the simultaneous reaction

17th

thermally conductive internals, heat pipes

18th

Combustion chamber

19th

Regenerative heat exchanger with periodic change of flow direction

Claims (9)

1. Integrated reactor for the autothermal coupling of exothermic and endothermic reactions with separate guidance of the two reaction streams, characterized in that the cold feeds 1 , 4 , 8 of each of the two reaction fluids in heat exchangers 2 , 9 through hot processes 3 , 10 with approximately the same heat capacity as the inlet are preheated, suitable measures prevent a pre-reaction of the reaction fluid of the exothermic reaction in the heat exchanger 2 is avoided and both fluids enter separate sections 11 , 12 of a reaction chamber 7 , which are designed so that in the respective reaction takes place and there is an intensive heat transfer between the two fluids and parallel to the main flow direction, so that local overheating conditions of the fluid for the exothermic reaction and local supercooling of the fluid for the endothermic reaction are largely avoided and the hot processes run out the reaction chamber 7 for preheating cold inlets can be used. 2. Integrated reactor for the autothermal coupling of exo- and endothermic reactions in a reaction medium ("simultaneous reaction control"), characterized in that the cold incoming reactants 4 , 13 are preheated by the hot products 15 in heat exchangers 14 , whereby Suitable measures an exothermic pre-reaction of the fluid 13 is avoided in the heat exchanger and the fluid 13 after preheating enters a reaction chamber 16 which is designed so that the two exothermic and endothermic reactions occur largely simultaneously in it, so that the the exothermic reaction released heat of reaction is taken up as directly as possible by the endothermic reaction without major temperature differences occurring over the length of the reaction space and the outlet from the reaction space 16 heating the feeds. 3. Integrated reactor for the autothermal coupling of exothermic and endothermic reactions, the heat required for the endothermic reaction being generated in that the hot product fluid of the exothermic reaction is admixed to the reaction mixture of the endothermic reaction, characterized in that for each of the two reaction fluids the cold inlet 1 , 8 is preheated in a heat exchanger by a hot outlet of approximately the same heat capacity, with suitable measures being avoided that the components supplied for the exothermic reaction already react in the heat exchanger and the preheated fluid for the exothermic reaction in a combustion chamber 18 reacts while the preheated reaction mixture of the endothermic reaction enters a reaction chamber 12 and is mixed there with the hot product from the combustion chamber 18 , the reaction chamber 12 being designed in such a way that an intensive heat transfer in parallel to the main stream direction and a quick and complete mixing takes place and part of the hot discharge from the reaction chamber 12 is used for the heat exchange with the cold feed of the reactants for the exothermic reaction. 4. Integrated reactor for the autothermal coupling of exothermic and endothermic reactions according to claims 1 to 3, characterized in that the heat exchanger described there between the cold inlet and the hot outlet of the reaction chamber as a countercurrent or cross / countercurrent heat exchanger 2 , 9 , 14 in a known tube bundle or plate pack construction or as a regenerative heat exchanger 19 with fixed or rotating storage beds, and a pre-reaction of the inflowing reactants of the exothermic reaction in the heat exchanger is avoided in that no catalytically active materials are installed in this heat exchanger path or that one the reaction partner 4 required for the exothermic reaction is conducted separately from the other reaction partners and for the products emerging from the reaction space for the endothermic reaction 12 , 16 in the heat exchanger 9 , 14 , 19 catalysts can be arranged for a suitable after-reaction can. 5. Integrated reactor for autothermal coupling of exothermic and endothermic reac tions according to claim 1 to 4, characterized in that there for the Reaction chamber required intensive heat transfer parallel to the main stream direction through highly heat-conducting internals, through heat pipes (heat pipes) or with a meandering or spiral flow good heat exchange or by circulating a particulate moderate, liquid or gaseous heat transfer medium is achieved. 6. Integrated reactor for the autothermal coupling of exothermic and endothermic reactions according to claim 1 to 5, characterized in that the reaction chambers described there 11 , 12 or 16 are designed as a fluidized bed apparatus, the fluidized material having catalytic or inert properties and the catalyst can also be arranged on the walls or on fixed internals and the feeds 1 , 5 , 6 , 8 and 13 open into the fluidized bed in such a way that a rapid, uniform distribution of the inlets over the entire fluidized bed occurs. 7. Integrated reactor for autothermal coupling of exothermic and endothermic reac tion according to claim 1 to 6, characterized in that local overheating fluid for the exothermic reaction and local supercooling for the s dothermic reaction e.g. B. as a result of a separation of the reaction zones be reduced or avoided that the heat demand rate of the endothermic Reaction and the heat production rate of the exothermic reaction to each other be adjusted so that the largest possible overlap area between endothermic and exothermic reaction zone. 8. Integrated reactor for the autothermal coupling of exothermic and endothermic reactions according to claim 7, characterized in that the required alignment of the heat demand and production rates by influencing the catalyst activity by inert admixture or by a sequence of catalytically active and inert areas and / or by adjusting the entry temperature into the reaction space 7 either separately only for the exothermic or the endothermic reaction or for both together. 9. Integrated reactor for the autothermal coupling of exothermic and endothermic reactions according to claim 7 or 8, characterized in that the avoidance or reduction of strong temperature fluctuations in the reaction chamber is caused by that the reaction mixture 1 for the exothermic reaction and the reaction mixture. 8 flow through the reaction chamber 7 in cocurrent for the endothermic reaction.