DE2751251A1 - CATALYTIC REACTOR PLANT - Google Patents

Description

The invention relates to a catalytic reactor system, which is used, for example, to generate product gases from serves a charge.

Catalytic reaction systems for converting hydrocarbon fuels into usable technical gases, such as, for example, hate carbon, are known. They are generally designed for a high yield of product gas. Plant size is generally of secondary importance since the cost of producing the product gas is a small fraction of the price of the products made from the product gas. The most common method of producing hydrogen is steam reforming

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mating or steam reforming of a hydrocarbon fuel by passing it through reaction or reactor tubes filled with a heated catalyst and are arranged within a furnace. Typically the reaction tubes are 6.1 to 12.2 m long and the Heat transfer occurs mainly (on the order of 70%) by radiation from the furnace walls on the reaction tubes. This requires a relatively wide gap between the tubes and the mount of the tubes next to the walls of the oven so that each tube is heated evenly by radiation from the walls will. These technical hydrogen generation plants have a very high heat transfer efficiency on the order of 5 4260 to 67 825 kcal / m of reaction tube surface area and per hour. However, this type of plant is mainly dependent on radiant heat and the thermal reactor efficiency is only 40 to 60%. It is true that high hydrogen conversion capacities can be achieved, a large one However, the percentage of thermal energy generated in the furnace leaves the furnace in the form of high temperature exhaust gases (i.e. in the form of heat loss). Large amounts of fuel must therefore be burned in order to achieve high heating outputs. If the thermal energy is not used in a separate process, for example to generate steam, must they are dissipated as lost energy. Even if the lost heat is used, it will not be used for generation of hydrogen, thereby reducing the thermal efficiency of the reactor and reducing the cost of the hydrogen produced increase.

Together with the development of fuel cell power plants, the need for cheap hydrogen as fuel and the need for low plant costs arose in order to be able to make fuel cell power plants economically competitive with existing power generation plants. This need created an additional incentive

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Reduce the size and operating costs of fuel processing plants for the production of hate carbon from hydrocarbon fuels. U.S. Patents 3,144,312 and 3,541,729 describe attempts to reduce the size of reactor systems and to increase the thermal efficiency. The extent to which these attempts are successful if they were successful at all, it cannot be easily ascertained. In the following description however, the disadvantages of the constructions known from these US patents are compared with the invention set out.

U.S. Patent 3,909,299 describes a steam reforming reactor design which, while having some desirable features, but which can neither be as effective nor as compact as the system according to the invention described below.

The aim of the invention is to create a catalytic reactor system which can operate with high thermal reactor efficiencies and which has a compact structure.

The invention provides a catalytic reactor system that is both compact and has high thermal reactor efficiencies and is able to work with high heating outputs.

The catalytic reactor system according to the invention contains an annular reaction chamber which is located within a furnace is arranged, with heat for the reaction by 1) hot furnace gas flowing in countercurrent to the flow through the reaction chamber within a narrow ring which is coaxial to and adjacent to the outer wall surface of the annular reaction chamber, and 2) by regenerative heat the reaction products that leave the reaction chamber and flow in countercurrent to the flow through the reaction chamber within a narrow ring which is coaxial is arranged to and next to the inner wall of the reaction chamber

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and carries the reaction products generated by the heating pads of the hot gases within the furnace are substantially isolated. The invention is particularly suitable for a large To accommodate number of reactors in a compact furnace volume

To achieve low costs, high heating outputs (i.e. high speeds at which heat from the hot gases in the furnace on the reaction flow per unit of the wall surface area, which separates the two streams from each other, is transmitted) and a compact arrangement is required. A high thermal reactor efficiency requires a high rate of conversion of process fuel to hydrogen with a minimal amount of fuel burning in the furnace. Elaborate and expensive constructions to avoid from excessive thermal stresses caused by temperature differences generated between connected parts should not be required.

All of this is achieved by the invention, according to which two streams are used to heat the reaction stream. The main source of heat is the countercurrent flow of furnace gases through a narrow ring along the outer wall of an annular reaction duct. The other heat source is regenerative heat from the reaction products, which leave the annular reaction chamber and flow in countercurrent through a narrow ring along the inner wall of the same. The use of counter-currents and narrow annular hot gas channels are critical factors in maximizing heating power and reactor thermal efficiency. A high regenerator heat transfer efficiency reduces the furnace heating power required per unit of process fuel supply. It can therefore be processed more fuel at the same amount of used fuel in the kiln (that is, the system works with a higher overall thermal efficiency). In this regard, the size of the ring

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gap from each of the two annular channels carrying hot gases into heat exchange relationship with the reaction chamber lead, a critical factor in determining how much of the available heat is actually in the heating currents is transferred to the reaction stream.

In order to illustrate the invention it is useful to consider a parameter referred to as heat transfer efficiency, c. The heat transfer efficiency is equal to the change in enthalpy of the heating current divided by the theoretical maximum change in enthalpy. In other words, if the heating stream has an enthalpy E- at its inlet _{temperature T 1} and an enthalpy E ₂ at its outlet temperature T ₂ , and if the heated stream has a temperature T ₃ at its inlet , the heat transfer efficiency between the two streams is through given the following equation!

where E _{3 is} the enthalpy of the heating current, calculated at temperature T ₃ .

It is also important to define the thermal reactor efficiency η:

(N "). (LHV ")

^{H H}

(F _r ) (LHV _r ) + F _f (LHV _f )

where N _{11 is} the total amount of hydrogen produced, LHV “H ₂ H ₂

is the lower calorific value of hydrogen, F _{r is} the amount of process fuel fed to the reactor, F is the amount of fuel fed to the furnace, and where LHV and LHV- are the lower calorific values of the process fuel and the furnace fuel, respectively . It has been assumed above that hydrogen is the desired reaction product. The equation can easily be modified for other reaction products.

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It should always be kept in mind that η is approximately directly proportional to c and that therefore a high degree of efficiency requires a high degree of heat transfer efficiency.

The advantage of the reactor system according to the invention is mainly that it has a high thermal reactor efficiency has a wide range of heating outputs (including very high heating outputs), while the Plant is compact in size. The result is a durable, compact, economical and effective construction, which is able to work with high process fuel throughputs to work.

Several embodiments of the invention are in the drawings and are described in more detail below. Show it:

Fig. 1 is a partial vertical sectional view of a

catalytic reactor system according to the invention, and

FIG. 2 shows a cross section through the plant from FIG

FIG. 1 essentially on line 2-2 of FIG. 1.

The catalytic reactor system 10 of FIGS. 1 and 2 is considered to be an exemplary embodiment of the invention. In this The system is used for steam reforming of a reformable hydrocarbon fuel in the presence a suitable catalyst to generate hydrogen. The system 10 includes a furnace 12 with burner nozzles 14, with a burner fuel manifold 16 and with an air manifold 18. Inside the furnace 12 are several tubular ones Reactors 20 arranged.

Each reactor 20 has an outer cylindrical wall 22 and

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an inner cylindrical wall or central tube 24 defining an annular reaction chamber 26 between them. The reaction chamber 26 is filled with steam reforming catalyst pellets 28, which rest on a grid 30 that is attached to the inlet 32 of the reaction chamber is arranged. Any suitable steam reforming catalyst such as Nickel, can be used to fill the reaction chamber from its inlet 32 to its outlet 36. The cylinder that is limited by the outer wall 22 is closed at its upper end 38 by an end cap 40. The central tube has an upper inlet end 42 and a lower outlet end. The inlet end 42 terminates below the end cap 40 so that the central tube in gas communication with the outlet 36 of the reaction chamber 26 is.

Inside the central tube 24, a cylindrical plug is arranged, the outer diameter of which is slightly smaller than the inner diameter of the center tube, creating an annular regeneration chamber 48 between the plug and the center tube is formed which has an inlet 49. The plug 46 can indeed be a solid rod, in the case of the one described here Embodiment, however, it is a tube which is closed by an end cap 50 at one end, so that Reaction products leaving the reaction chamber 26 flow around the plug 46 through the regeneration chamber 48 have to. The distance between the plug 46 and the central tube 24 is maintained by bulges 52 in the plug wall.

In the invention, the regeneration chamber 48 serves the purpose of returning heat from the reaction products which leave the outlet 36 to the catalyst bed of the reaction chamber 26. Therefore, with regard to the invention, the outlet 54 of the reaction chamber 48 is positioned adjacent to the inlet 32 of the catalyst bed rather than at the outlet end 44 of the central tube.

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see, despite the fact that the actual Ring formed between plug 46 and central tube 24 extends to outlet end 44. the The arrangement shown in Fig. 1 ensures a certain preheating of the process fuel before it enters the catalyst bed entry. However, this is not critical for the present invention. In addition, in this embodiment the plug 46 over the entire length of the reaction chamber, so that the inlet 49 of the regeneration channels is adjacent the outlet 36 of the reaction chamber is located. While this is preferred for maximum regeneration, the regeneration chamber inlet however, it can be placed anywhere between the inlet and the outlet of the reaction chamber by a shorter stopper is used.

It should be noted that the regeneration chamber 48 is substantially isolated from the hot furnace gases. To achieve For maximum overall reactor efficiency, it is important to prevent the thermal energy of the furnace gas from removing the reaction products to be heated within the regeneration chamber 48. It is also important to avoid burning extra Prevent fuel or hydrogen within the regeneration duct 48. Only inherent heat that is already in the reaction products present at outlet 36 is transferred to the reaction chamber.

Each reactor 20 can be viewed as a reactor having an upper part 56 and a lower part 53. The upper part 56 is arranged in a space which is referred to below as the combustion chamber 60. The combustion chamber 60 is that volume of the furnace 12 within which the actual combustion of the fuel and the air introduced into the furnace takes place. This space is characterized by very high temperatures, considerable radiant heating and convection heating of the reactors 20 and by axial (ie in the direction of the axis of the reactors 20) and radial

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Mixing the gases marked therein.

The lower part 58 of each reactor is surrounded by a cylindrical wall 62 which is arranged at an external distance from the wall 22 is and with this an annular burner gas channel 64 with an inlet 66 and an outlet 67 is limited. The outlet 67 is adjacent the inlet 32 of the reaction chamber 26. The channel 64 is lined with a heat transfer packing material filled, which rests on a grid 68 and in the present example consists of balls 70 made of aluminum. The space between adjacent cylindrical walls or channels 62 is covered with a non-thermally conductive material such as a ceramic fiber insulation, filled, which rests on a plate which extends over the furnace and in which holes are formed through which the reactors 20 pass. The plate 74 and the material within the space 72 prevent the furnace gases from flowing around the outside of the cylindrical walls or channels 62.

In addition to plate 74, plates 76, 78 and 80 also extend over and delimit the oven Distributor. The plate 80 rests on the bottom wall 82 of the oven. The plates 78 and 80 define a reaction product manifold between them 84. Plates 76 and 78 define a process fuel inlet manifold 36 therebetween. Plates 74 and 76 define a furnace gas outlet manifold 88 therebetween. Plugs 46 and center tubes 24 butt against the base plate 80. The outer walls 22 of the reactors abut the plate 78. The cylindrical walls or Channels 62 abut plate 74.

In operation, a mixture of steam and reformable hydrocarbon fuel enters the inlet 32 of the reaction chamber 26 from the manifold 86 through holes 90 in the wall; the distributor 86 is supplied via a line 92. Immediately

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the mixture begins to be heated by the furnace gases flowing in countercurrent to it through channel 64, and the mixture begins to react in the presence of the catalyst particles 28. When the fuel, steam and reaction products move upward within the reaction chamber 26, they continue to react and absorb additional heat. At the outlet 36 the temperature of the reaction products reaches a maximum. The hot reaction products enter the inlet 49 of the regeneration chamber 48. When the reaction products spread over the length of the annular regeneration chamber move away, heat is returned from them to the reaction chamber 26. You then enter the reaction product distributor 84 through holes 94 in the central tube 24 and are fed via a line 96 for further processing, for storage or carried away from the reactor for consumption.

Fuel for the furnace enters the manifold 16 via a line 98 and then passes through the nozzles 14 into the combustion chamber 60. Air enters the manifold 18 via a line 100 and passes through annular passages 102 that surround each nozzle 14, into the combustion chamber 60. The combustion of the fuel and the air takes place within the combustion chamber. The hot gases from the combustion chamber move through the channels 64 into the distributor 88 and are discharged via a line. The temperatures within the combustion chamber are generally sufficiently high so that high heating outputs are achieved in the region of the upper parts 56 of the reaction chambers despite the relatively low heat transfer coefficient in this region. If the temperature of the furnace gases drops while the gases move away from the burner nozzles, the heating output would normally become unacceptably low. However, according to the invention, this is counteracted by the use of the annular burner gas channels 64 above the lower parts of the reactors. These channels increase when they do

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correctly dimensioned, the local heat transfer coefficient and therefore the heat transfer efficiency values. This leads to high heating outputs both over the top Parts as well as above the lower parts, despite the lower temperatures of the furnace gases in the area of the lower parts Parts.

The size of the annular gap in the burner gas duct, the Reaction chamber and the regeneration chamber. According to the invention, these gaps are dimensioned so that the highest possible heat transfer efficiency results, which with the desired exhaust gas temperatures of the furnace gases and the reaction products is compatible. Although theoretically the heat transfer efficiency increases with a narrowing burner gas channel and with a decreasing regeneration chamber gap size practical limit values, such as the maximum allowable wall temperatures and pressure drops within the rings, are important factors when determining the minimum permissible gap sizes for a special application. The size of the annular gap in the reaction chamber is combined with the size of the gap in the burner gas duct and the regeneration chamber selected so that sufficiently high temperatures result in the entire catalyst bed, without furnace gases in the burner gas channel, the reaction products within the regeneration chamber 48 on the other Heat the side of the catalyst bed. The regeneration chamber 48 must, as already mentioned above, withstand the effects of heat the furnace gases are essentially isolated.

At this point, it is interesting to compare the invention with the plants that are known from the aforementioned US Patents 3,541,729 and 3,144,312. In the plant known from US Pat. No. 3,541,729, the furnace heating stream flows in the same direction as the stream through the annular catalyst bed along the inner wall thereof. This solution is clearly less

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effective and differs from the countercurrent which, according to the invention, goes along the outer wall of the bed. In the plant known from US Pat. No. 3,541,729, the highest furnace gas temperatures prevail at the inlet end of the catalyst bed, which is the coolest end, and the heat transfer in that area is probably so great that a significant amount of the heat from the furnace gases is applied to the tops of the regeneration stream in the ring 113 is transmitted. This heat leaves the furnace along with the reaction products, thereby increasing the overall thermal efficiency of the reactor is decreased. This is not the case with the invention because the burner gas is at the reaction chamber inlet is coldest due to the countercurrent.

The system known from US Pat. No. 3,144,312 differs from the plant according to the invention in that the furnace gases are located on the inner annular catalyst bed. In addition, the furnace gases flow alongside both the inner and the outer reaction stream, which is in contrast to the Invention stands in which the regeneration stream is substantially isolated from the hot furnace gases, which is in accordance with the invention is an important requirement. It should also be noted that the relatively cool cylindrical outer wall 10 on the relatively hot inner cylindrical wall 9 is rigidly attached. Stresses caused by different thermal expansion between these two walls are likely to be unacceptably high and can cause interference. Furthermore, none of the systems known from the two US patents is suitable for use with multiple reactors in suitable for a single oven.

Returning to the present invention it is noted that it has been found that a relatively narrow range of gap sizes results in good thermal reactor efficiencies at both high and low process fuel throughputs. The heat transfer packaging material 70 contained within

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of the channels 64 provides a further improvement in heat transfer efficiency and uniformity of heat distribution compared to a ring of the same size but without heat transfer packing material. Since the heat transfer efficiency increases with decreasing size of the annular gap, the heat transfer packing material of the invention could be omitted if the size of the annular burner gas channel were reduced. While this is within the scope of the invention, a wider annular channel of heat transfer packing material is preferred because it is more difficult and expensive to maintain dimensional tolerances as the gap becomes smaller. Acceptable ranges for gap sizes with and without heat transfer packing material are given in Table 1, while best results obtained using the preferred ranges are given in Table 2. The ranges given are reliable estimates based in large part on test results. It should be noted that the specified ranges can be extended for reactors with very small or very large diameters.

TABLE 1 Permissible annular gap sizes

Reaction chamber 7.6 - 50.8 mm Regeneration chamber 2.5 - 25.4 mm Burner gas duct 2.5 - 25.4 mm (without packing material) Burner gas duct 12.7 - 76.2 mm (with packing material)

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TABLE 2
PREFERRED RING GAP SIZES

Reaction Kanuner Regeneration Kanuner Burner gas duct (without packing material)

Burner gas duct 12.7 - 50.8 mm

(with packing material)

12th , 7 38 ,1 mm 3 , 2 12th , 7 mm 6th , 4 12th , 7 well

Some other factors that determine the choice of gap size are: properties of the gases and catalyst particles, the thickness and the thermal conductivity of the walls which separate the heating gases and the heated gases from one another, and the Reynolds numbers of the various streams. The walls that the countercurrents separate from each other, are usually made as thin as possible, as it is with the structural Withstands integrity, and made from materials that are not very expensive but have good thermal conductivity. The catalyst is generally chosen to have good reactivity and long life. The catalyst particle size is generally chosen to be as small as possible in order to maximize the catalyst surface area, but not so small that an unacceptable pressure drop is created in the reaction channel.

Although not shown in the drawings, means should be provided which prevent fluidization of the catalyst bed as a result of the upward flowing process gas.

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Example I;

In a steam reforming reactor plant similar to that of Figs with nineteen tubular reactors, each reactor was approximately 1524 mm in length as measured from inlet 32 and one Outside wall diameter of 229 mm. Half the length (762 mm) of the reactor extended into combustion chamber 60. The outer walls 22 of adjacent reactors were spaced apart by 76 mm. The reactors on the furnace wall were between 102 mm and 127 mm away from it. The gap between the The outer wall 22 and the inner wall 24 were 27.9 mm, that between the inner wall 24 and the plug 46 was 6.4 mm, and that between the cylindrical wall 62 and the outer wall 22 was 31.8 mm. The burner gas channel was filled with 12.7 mm diameter Raschig rings made of alumina. The catalyst was in the form of cylindrical pellets. The process fuel was naphtha, which was used in the catalyst bed as a about 4.5 parts by weight of steam mixed steam entered. The process fuel throughput was about 11.3 kg / h per reactor with a total fuel throughput of about 215 kg / h. A conversion efficiency of 95% and an overall thermal reactor efficiency of 90% were achieved.

Example II;

In a steam reforming reactor according to the invention with a In a single tubular reactor, the reactor length was 1524 mm, measured from inlet 32, and the reactor had an outer wall diameter of 229 mm. Half the length (762 mm) of the reactor extended into the combustion chamber 60. The furnace wall was spaced 76 mm from the outer wall of the reactor all around. The gap between

the outer wall 22 and the inner wall 24 was 27.9 mm, that between the inner wall 24 and the plug 46 was 6.4 mm and that between the cylindrical wall 62 and the outer wall 22 was 31.8 µm. The burner gas duct was made of aluminum

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oxide balls with a diameter of 12.7 mm. The catalyst was in the form of cylindrical pellets. The process fuel was naphtha, which was used in the bed as one about 4.5 parts by weight of steam mixed steam entered. The process fuel throughput was 12.7 kg / h. One Conversion efficiency of 88% and an overall thermal reactor efficiency of 87% were achieved.

The manifold arrangement and burner construction shown in the drawings are exemplary only and are not critical to the invention or to any part thereof, since the invention is within a single reactor of a furnace as well as many reactors, as the previous examples have shown. The invention brings however, there are particular advantages when several reactors are arranged in a single furnace, since it allows to pack the reactors tightly by providing both an even and extremely effective heating of the lower Secures parts of the reactors.

Tightly packed reactors or reactor tubes, as this term is used here and in the claims, represent a non-linear one regular arrangement of at least three reactors, the arrangement essentially filling the combustion chamber volume and the reactors being substantially evenly spaced and substantially equally and closely spaced from one another are arranged within the combustion chamber volume. For example, assuming a cylindrical combustion chamber, pinhole order made up of three closely packed reactors in the shape of an equilateral triangle, with one reactor at each Corner. An array of four closely packed reactors can be in the shape of a square, with one reactor at each corner. An array with five reactors can contain a central reactor, which by a square arrangement of four reactors

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ren is surrounded. Nine reactors can have a square arrangement from three parallel rows with three reactors each. A hexagonal arrangement with nineteen reactors is shown in FIG. In all cases, at least a portion of each reactor in the assembly receives a substantially smaller one Amount of direct radiation from the combustion chamber wall. For example, reactors on hand receive much less Radiation on the side facing away from the hand. In addition, parts of the reactors receive a much smaller amount Amount of radiation due to the blocking of radiation by other reactors in the array.

The invention is not limited to the steam reforming of hydrocarbon fuels to produce hate carbon. The heat transfer principles on which the invention is based could just as easily be applied to other endothermic catalytic reactions.

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Claims (10)

Patent claims: A catalytic reactor system characterized by a combustion chamber for burning fuel to produce hot gases; by at least one tubular reactor with a first part that extends into the combustion chamber, with an outer wall and with an inner wall, the inner wall being arranged at a distance from the outer wall and with this delimiting an annular reaction chamber for receiving a reaction catalyst, the reaction chamber has an inlet end and an outlet end and wherein the outlet end is located in that part of the reactor which extends into the combustion chamber; by a wall arrangement which is spaced from the outer wall of the reaction chamber and with this delimits a narrow annular burner gas channel which extends coaxially to and next to the reaction chamber and has an inlet end in gas communication with the combustion chamber and an outlet end substantially at the inlet end of the reaction chamber has, wherein the burner gas channel is intended to deliver hot gas from the combustion chamber via the 809826/0530 Outer wall of the reactor in countercurrent to that through the reaction chamber directing current therethrough to add heat thereto; and by a device that with distance is arranged inwardly of the inner wall of the reactor and with this a narrow annular regeneration chamber limited, which is arranged coaxially to and adjacent to the annular reaction chamber and an inlet end and an outlet end with the inlet end of the regeneration chamber for receiving all reaction products from the reaction chamber outlet end is intended and wherein the regeneration chamber is intended for the reaction products in countercurrent to conduct the current passing through the reaction chamber and only inherent heat that is already in the reaction products is present at the outlet end of the reaction chamber to transfer back into the reaction chamber. 2. Reactor plant according to claim 1, characterized in that that the inner wall of the reactor delimits a cylindrical channel coaxially to the annular reaction chamber and that with Distance inwardly from the inner wall of the reactor arranged device is a cylindrical plug which is inside the Channel is arranged and has an outer wall surface that is spaced is arranged inward of the inner wall of the reactor and with this delimits the annular regeneration chamber. 3. Reactor plant according to claim 1 or 2, characterized in that the distance between the walls of the regeneration channels is between 2.5 mm and 25.4 mm, that the distance between the walls of the burner gas channel is between 2.5 mm . and 76.2 mm and that the distance between the walls of the reaction chamber is between 7.6 mm and 50.8 mm. 4. Reactor plant according to one of claims 1 to 3, characterized in that the reaction chamber contains a steam retormierkatalysator and that the reactor plant means for introducing a reformable hydrocarbon f- 809826/0530 fuel and water vapor into the reaction chamber inlet end and means for introducing a fuel and an oxidizing agent in the combustion chamber. 5. Reactor plant according to one of claims t, 2, 4 or 5, characterized characterized in that the burner gas duct is substantially filled with a heat transfer packing material. 6. Reactor plant according to one of claims 1 to 5, characterized in that the distance between the walls of the Hc-yenerationskammcr is between 3.2 mm and 12.7 mm that the distance between the walls of the burner gas channel is between 12.7 mm and 50.8 mm and that the distance between the Walls of the reaction chamber between 12.7 mm and 38.1 mm. 7. Reactor plant according to one of claims 1 to 6, characterized in that the reactors are vertical within the furnace are arranged and that the outlet end of the reaction chamber is at the upper end of the reaction chamber. 8. Reactor plant according to one of claims 1 to 7, characterized characterized in that a plurality of tubular reactors are arranged within the furnace, that each reactor has an inner and an outer wall arrangement having an annular reaction chamber between them for receiving the reaction catalyst limit that each reaction chamber has a first part and a second part and an inlet end and a Outlet end has that the first part has the outlet end and is arranged within the combustion chamber that the second part is arranged outside of the combustion chamber that each reaction chamber is assigned a device which coaxial with her and next to her a narrow annular regeneration chamber bounded, the inward of the distance Reaction chamber is arranged and has an inlet end and an outlet end, the inlet end of which all reaction products from the reaction chamber outlet end passing through the regeneration chamber in countercurrent to that through 809826/0530 Current passing through the reaction chamber is conducted to only the inherent heat that is already in the reaction products is present at the outlet end of the reaction chamber to transfer back into the reaction chamber that second part each reaction chamber has an associated wall arrangement which is arranged at a distance outside it and which is coaxial with it delimits a narrow ring-shaped burner gas channel extending over the length of the second part and next to it, which has an inlet end in gas communication with the combustion chamber and an outlet end and hot gas from the combustion chamber to the The outlet end of the channel in countercurrent to the flow passing through the reaction chamber in order to supply heat thereto, and in that the furnace is provided with means to prevent the hot gas in the combustion chamber from being different than leaves through the annular burner gas channels. 9. Reactor plant according to claim 8, characterized in that the regeneration chamber is essentially on the extends the full length of the reaction chamber. 10. Catalyst according to claim 8 or 9, characterized in that the device assigned to the reaction chamber, which delimits the regeneration chamber with it, is a cylindrical plug that has a cylindrical outer surface, which is at a distance from the inner wall arrangement of the reactor and with this delimits the regeneration chamber. 809826/0530