DE102015122129A1 - Reactor for carrying out exo- or endothermic reactions - Google Patents

Abstract

The invention relates to a reactor and a process for reacting a gaseous and / or liquid reaction medium with at least two reaction spaces at least partially filled with a catalyst, which are formed by arranging in the reactor at least three heat transport spaces arranged substantially parallel to one another. so at least partially separate the individual reaction spaces from each other. The heat transport spaces are each formed by at least one thermal blanket, wherein each thermal blanket consists of two sheets which are interconnected at the edges and a plurality of further positions above the surface. In operation, the horizontal extent of the reactor in at least one axis is greater than its vertical extent. In addition, the inlet and the outlet for the reaction medium are provided so that the reactor is vertically flowed through by the reaction medium.

Description

The invention relates to a reactor for reacting a gaseous or liquid reaction medium with at least two at least partially filled with a catalyst reaction spaces, which are formed by the fact that in the reactor at least three substantially mutually parallel heat transfer spaces are provided, so the individual reaction spaces at least partially each separate, wherein the heat transport spaces are formed by at least one thermal blanket and wherein each thermal blanket consists of two sheets, which are welded together at the edges and on the surface of a plurality of spot welds, which also connect the plates are distributed. Likewise, the invention also relates to a method for carrying out the reaction in such a reactor.

A number of typical heterogeneously catalyzed exothermic gas phase reactions are carried out in so-called fixed bed reactors. In each case, a bed (fixed bed) of catalyst particles or catalyst-coated carriers is flowed through with the reaction medium. Subsequently, the reaction medium flows through a heat exchanger to at least partially remove the heat of reaction formed before it enters the next catalyst bed. Alternatively, the temperature reduction can also be realized by introducing a material flow for quenching. Overall, typical reactors have 4 to 6 fixed beds, which are flowed through in succession.

Using the example of a conversion of methanol to propylene (MTP process), the design of such fixed bed reactors will be explained in more detail. 1 shows a reactor as commonly used for the conversion of methanol to propylene. The reactor 10 is over the line 13 and 13 ₁ fed methanol overhead. From there, in the direction of earth's gravity, it first hits the fixed bed 11 ₁ where at least parts of the methanol are converted to propylene. Since the reaction is exothermic, while heat of reaction is released in the heat exchanger 12 _{1 is} discharged. Alternatively, the temperature reduction can also be realized by introducing a material flow for quenching. The desired temperature before entering the subsequent fixed bed 11 ₂ can also be achieved by adding a suitably conditioned material stream (eg methanol) as a quench stream.

Subsequently, the mixture of oxygenate, preferably methanol, propylene and other reaction products enters the fixed bed 11 _{2 on} . Usually here is a line 13 ₂ again fresh oxygenate above the actual fixed bed fed, whereby the conversion in each fixed bed and thus also the amount of heat can be additionally controlled. Subsequently, the educt-product mixture through the heat exchanger 12 ₂ led. The same thing is repeated in the fixed beds 11 ₃ , 11 ₄ , 11 ₅ and 11 ₆ and the corresponding heat exchangers 12 ₃ , 12 ₄ , 12 ₅ and 12 ₆ and the supply lines 13 ₃ , 13 ₄ , 13 ₅ and 13 ₆ . Finally, the product mixture is passed over line 14 deducted.

In a typical MTP system, three of these reactors are provided, of which two are operated in parallel and the third is in stand-by or the catalyst is being regenerated. A typical design of such a plant and method can be found in the DE 1 002 7159 or even the US 2009/0124841 , After completion of the catalyst regeneration, the reactor with the regenerated catalyst is put back into operation, while the reactor, which includes the catalyst with the longest life, now the regeneration is supplied. So there are thus always in a typical production line 2 reactors in the operating mode, which carry out the reaction, but which are filled with catalysts with different aging states.

The present reaction concept requires a large reactor volume of about 2000 m ³ (for a plant capacity of about 450 kta of propylene), which results from the fact that in addition to the adiabatic catalyst beds already mentioned cooling zones must be provided in the form of heat exchangers or quench sections. In addition, appropriate space must be provided for the filling and emptying of the catalyst.

As a rule, six fixed beds are arranged one above the other, each having a height of 20 to 60 cm. In each reactor, about 150 M of catalyst is distributed over these six catalyst beds, with the total amount of catalyst rising above the beds. This means that less catalyst is to be found in the first bed, so that here the reaction can not run completely targeted, but is limited by the amount of catalyst. This is to prevent a runaway reaction due to excessive local heat production by exothermic reactions. By including the last, the sixth bed, the largest amount of catalyst, it can be ensured that the methanol is completely or almost completely reacted.

Usually there are about 100 compartments in each fixed bed, which are individually filled with catalyst. This method is compared to the inventive concept (only 1 bed) as relatively expensive. In the flow through the fixed bed with the catalyst is to ensure that later all subjects are flown evenly to avoid local catalyst damage. In addition, it must also be avoided that the catalyst comes into contact with liquid, as this can lead to permanent damage to the catalyst. In addition, to adjust the temperature in each fixed bed, partially reacted reaction medium is mixed with fresh reaction medium.

Furthermore, it must be ensured in the reactor that the lowest possible pressure loss occurs over the fixed bed, so as to ensure the selectivity towards the target products, the short-chain olefins, especially propylene.

As explained above, the current reactor concept requires a comparatively large reactor volume and reactor diameter for the usual propylene capacity of more than 450,000 t per year in order to keep the pressure loss low. Therefore, the reactor can not easily be designed even larger and also construction and transport are limited.

In summary, there is therefore definitely room for improvement in the plant construction described, in particular with regard to the very large reactor volume and diameter, the demanding distribution of the reaction medium and the relatively complex handling of the catalyst.

It is therefore an object of the present invention to provide a smaller sized reactor in which exothermic reactions, in particular the MTP reaction can be carried out, with a uniform temperature profile at low pressure loss is the aim of the design. In addition, the handling, especially the filling with new catalyst should be facilitated.

This object is achieved by a reactor having the features of claim 1.

Such a reactor for reacting a gaseous or liquid reaction medium comprises at least two reaction spaces at least partially filled with a catalyst. These reaction spaces are formed by arranging at least three heat transport spaces arranged substantially parallel to one another in the reactor. Essentially in the context of the invention means that the course of the heat transport spaces deviates by a maximum of +/- 20 °, preferably 10 °, particularly preferably 5 °, very particularly preferably 2 ° from one another. These individual, parallel heat transport spaces separate the individual reaction spaces at least partially from one another.

The heat transport spaces are formed by in each case at least one thermal blanket. A thermo sheet according to the invention consists of two sheets, which are connected at the edges, preferably welded together and on the surface of a plurality of additional compounds, preferably spot welds, which also connect the plates together, are distributed. Such plates can be produced automatically by robots or machines and thus at very reasonable prices. After welding, the sheets are expanded by a hydraulic forming, usually so the injection of a liquid under high pressure, whereby pillow-like channels between the sheets arise.

Both thermal energy can be supplied to and removed from the reaction via the heat transport spaces, with the focus on exothermic reactions in the following, in which a removal of heat energy is accordingly required.

The invention is now that in operation, the horizontal extent of the reactor in at least one axis is greater than its vertical extent. This means that the flow of the reaction medium is orthogonal to the horizontal axis of the reactor. The thermal sheets may be oriented parallel to each other on the horizontal axis or orthogonal to the horizontal axis in the reactor.

In comparison to the previous reactors, the arrangement in the reactor according to the invention changes. The inlets and outlets for the reaction medium are provided so that the reactor is vertically flowed through by the reaction medium. Preferably, the flow takes place in such a way that the flow direction runs with the gravitational force. This has the advantage that it can not come to structural changes in the fixed bed of the catalyst during the flow.

The inventive design of a reactor which is less in height than in width, offers a variety of advantages. On the one hand, in principle can be dispensed with different fixed beds with interposed heat exchangers, but the thermal plates are within a single fixed bed.

On the other hand, there are now dimensions that entail a significantly lower pressure drop, since the flow of the reaction medium must already be divided above the individual reaction spaces in order to pass through the individual reaction spaces. In each case, the reaction medium then only flows through a fixed catalyst bed with the vertical height of the reactor, instead of being passed through a plurality of fixed beds as in the previously customary embodiment. The term reactor vessel in the context of the invention means a container inside the reactor, which comprises at least the thermoplates and their interspaces and is at least partially, preferably completely filled with catalyst. The thus significantly reduced path of the reaction medium also entails significantly lower pressure losses. Due to the reduced path of the reaction medium and the overall conditions over the covered by the reaction medium reaction path are much more uniform than in a reactor design in which the reactor is flowed through over a much longer vertical distance. As a result, in the reactor according to the invention, the reaction procedure can be much closer to the ideal isothermal reaction conditions and thus fewer by-products and more desired product, for example propylene, can be formed.

Furthermore, the replacement of the catalyst is significantly simplified, since fewer beds, more preferably a bed instead of the usual, for example in the MTP process 6 fixed beds must be replaced. Furthermore, the reactor has a much smaller diameter, which greatly simplifies transport and construction.

Finally, such a reactor has the advantage that it makes a very simple configuration possible for larger and smaller capacities, since, starting from the critical amount of thermal plates of at least 10 thermal plates, which form 10 heat transport spaces, it can be assumed that the reaction conditions in each reaction chamber are the same and thus the number of reaction spaces directly from the amount of the desired product by simple multiplication is calculated. At the same time reactors can finally be manufactured, which implement a smaller amount, so that the reactor appears to be more useful, especially for small plants than the previous reactors, which required certain minimum dimensions. In particular, in the approach to generate methanol from renewable resources, which will inevitably lead to a decentralization of the further processing of methanol, this concept is promising. In principle, it is possible with this concept to realize capacities of less than 100 kt per year of propylene.

In addition, the so-called steaming, so pretreatment of the catalyst with steam, is greatly simplified with only a fixed bed, since only a fixed bed must be treated and so better control of the temperature profile during the steaming process is possible.

The reactor dimensions are preferably designed such that a human can work in it without problems and all parts are easily accessible. This simplifies maintenance in particular. However, smaller reactor dimensions are also possible, in particular for smaller production capacities.

Furthermore, it is preferred if the reaction spaces extend vertically over the extent of the heat transport spaces. In practice this means that in the lower part of the reactor, ie the area closest to the surface of the earth, only fixed catalyst bed is to be found, but not thermoplates, so that here the reaction is adiabatic. Since this is the area in which the reaction medium is already implemented to a large extent because it has already passed through the longest distance vertically through the fixed catalyst bed, can be achieved by the adiabatic reaction conditions at this point, a completion of the conversion.

In addition, it has turned out to be favorable if the additional connections, preferably points, of the thermal sheet lie on straight lines, a straight line being defined by the fact that the respectively adjacent weld points lie on a straight line. Preferably, the distance of the individual points, which lie on a straight line to each other, always the same distance d3 and the straight lines always have the same distance d5 to each other, so they are parallel. In this case, it is particularly preferred if the points on the individual straight lines are offset relative to one another, so that straight lines can only be detected within one dimension. This creates a system that equally sufficient channels for ensures optimal heat exchange and thus a uniform temperature over the entire thermal plate.

In a particularly preferred embodiment, the thermal sheets between the additional compounds, preferably spot welds, the already mentioned pillow-like channels, in which the maximum distance between the two sheets to each other is the distance d2. At the same time, the distance between two adjacent thermal sheets is referred to as d1. According to the invention, the distance d1 between the two adjacent thermal surfaces and thus thus this reaction space is always greater than d2, namely the maximum expansion of the thermoplate between two additional connections, preferably spot welds. At the same time, the distance d1 is always less than one hundred times the distance d2. It is therefore an aspect of the invention that the already mentioned advantageous isothermal reaction procedure can be ensured in particular if these two geometrical parameters are adapted accordingly.

It is particularly favorable if the distance and thus the width of a reaction space d1 is between 1.5 times d2 and 10 times d2. Especially for the production of propylene from methanol results in an optimized reaction, in which hotspots in fixed catalyst bed can be excluded as well as bodies that are so cold that there is no reaction or even the condensation of methanol.

One aspect of the invention is the integration of a device for removing the catalyst. This may be designed, for example, such that the support surface of the catalyst can be opened by a folding mechanism, so that the catalyst falls down. Another, particularly space-saving design provides to divide the bearing surface of the catalyst into at least two parts and store them on rails so that in each case a part of the support surface can be pushed under the other and so the catalyst falls by gravity down ,

Furthermore, it is a special feature of the invention that the thermal sheets are designed so that they are suitable for guiding a molten salt. In addition to an optimized guidance with regard to the temperature profile, the channels in the thermoplates are designed so that when shutdowns or decommissioning a virtually complete emptying of the cavities in the thermal sheets is ensured by gravity. After the apparatus has cooled, no solidified salt remains in the thermoplate and reduces the risk of damage to the thermoplate. The re-commissioning is thereby facilitated accordingly). The use of a molten salt has the advantage that the wall thickness of the thermal plates can be significantly lower than in the usual use of high-temperature steam as a heat transport medium, since the pressure load is correspondingly lower. This in turn greatly improves the heat transfer. At low pressures within the thermoplates, such as when using molten salts, it is preferable to choose wall thicknesses between 0.5 and 1.5 mm per sheet (thermo sheet consists of 2 sheets) - some manufacturers prefer not to go below 1 mm due to the design. For systems with high pressures, it is more likely to move between 1.5 and 3 mm wall thickness - larger than 3 mm is hardly possible, because it can no longer deform accordingly, but with 3 mm design pressures of well over 100 bar can already be realized become.

It is also also possible to use high-pressure steam as a heat transport medium, as is usually done when using thermoplates. Such high-pressure steam has a pressure of up to 100 bar and therefore has a corresponding heat capacity. Larger system composite systems are usually designed with steam systems with different pressures (high, medium and low steam), which are suitable for carrying energy between the individual system components and in some cases electricity is also obtained from steam produced. The integration of the reactor type according to the invention in such a high-steam system is therefore recommended, in particular in a plant network.

Another aspect of the invention provides that the reaction chambers filled with a catalyst bed and the associated heat transport spaces are dimensioned such that the reactor has at least one thermoplate per cubic meter of catalyst and / or at least 10 m ^{2 of} cooling surface per cubic meter of catalyst bed Cooling surface directly represents the surface of one of the two sheets of thermal blanket. This results in a surprisingly simple correlation with respect to the total amount of thermal sheets used.

A further embodiment of the invention provides that in individual thermal plates passage openings are provided from one reaction space to another, for example through holes within the Thermo sheets, wherein the two sheets are connected by a round weld at these holes tightly together. Through these additional openings, the reaction medium can mix over the reaction spaces, which partially the homogeneity of the product can be further increased.

Furthermore, the invention comprises a device in which the reactor provides a gas distribution device, through which the reaction medium is uniformly distributed to all reaction spaces. Such a gas distribution device of such a distribution device can either be a distribution chamber from which a multiplicity of openings (for example, these can also be slits extending, for example, longitudinal or transverse to the horizontal axis of the reactor) or nozzles, the reaction medium into the Flow reactor with its reaction spaces, whereby a very uniform distribution over all spaces Rektionsräume can be achieved. It is equally possible, without a distribution chamber, to introduce the reaction medium directly via nozzles above the reaction spaces, from where it is distributed to the various reaction spaces. In principle, it is possible to work with larger and smaller nozzle quantities and corresponding connecting valves and pipes, or to make the individual nozzles and the associated equipment larger. A large number of nozzles has the advantage that the distribution of the reaction medium can be optimized in terms of a uniform distribution as possible and also a higher flexibility in terms of different flow rates in different reaction spaces is possible.

The catalyst may also be partially placed through a corresponding grid or other device within the reaction spaces. This has the advantage that a support structure can be introduced, which is removable again together with the catalyst from the reaction spaces.

It is also advantageous to apply a net and / or an inert material above the catalyst in order to move the catalyst in that region which faces the inflow of the reaction medium, in particular where heat transfer space is not yet provided or if it is just starting, the heat flow is reduced. As a result, the catalyst can be additionally protected.

Furthermore, it is also possible to introduce inert material together with a catalyst bed so that the catalyst density in the bed is reduced and thus the local reaction rate is lowered. Also conceivable is a non-homogeneous catalyst bed, which additionally influences the local reaction rate.

The invention also provides a process for reacting a gaseous or liquid reaction medium in a reactor having the features of claim 11. In this case, such a reactor comprises at least two reaction spaces at least partially filled with a catalyst, through which the reaction medium flows. The reaction spaces are formed by at least three heat transport spaces arranged essentially parallel to one another, wherein a heat transport medium flows through the heat transport spaces.

The heat transport spaces each consist of at least one thermal blanket, wherein each thermal blanket in turn consists of two sheets, which are welded together at the edges and over the surface of a plurality of spot welds, which also connect the plates are distributed.

It is the object of the invention that the reaction medium flows through the reactor vertically, preferably in the direction of gravitational force, and that the horizontal extent of the reactor in at least one axis is greater than its vertical extent. This offers the advantage that loading and unloading with the catalyst is significantly simplified.

Furthermore, the reactor itself is much easier to handle due to an overall narrower diameter. Also, a reduced in terms of today's plant capacity reactor with a capacity of 100-250 kt per year or less on the example of a conversion of methanol to propylene is conceivable.

It is crucial that the catalyst bed is flowed so very homogeneous, an isothermal reaction is achieved and at the same time the pressure loss is lower than in a conventional reaction.

It is an aspect of the invention that the heat transport medium is conducted in cocurrent to the reaction medium. This has the advantage that the largest temperature difference between the reaction medium and the heat transport medium in the region of the entry of the reaction medium takes place in the reaction chambers, where locally also the highest conversions and thus with an exothermic reaction also the largest heat development exists.

However, it is also possible to supply the heat transfer medium in countercurrent or even in crossflow (depending on the arrangement of the thermoplates, which can be oriented both vertically and horizontally to the flow direction of the reaction medium), since a more homogeneous temperature profile can be generated overall.

Furthermore, any form of heat transfer medium of liquid or gaseous form may be used. Due to its usually higher heat capacity, preference is given to a liquid heat transport medium, more preferably a medium which evaporates within the thermoplates, as a result of which the additionally required enthalpy of vaporization permits an even more isothermal reaction

Preferably, individual regions of the reaction spaces are operated adiabatically, whereby the conversion can be further increased.

Finally, it is an embodiment of the invention that the process carried out in the reactor of the invention is at least partially conversion of methanol to propylene, which is a typical reaction in a fixed bed, which in the previous reactor arrangement is a very large reactor with the same associated disadvantages required.

Other features, advantages and applications of the invention will become apparent from the following description of the drawings and the examples. All described and / or illustrated features alone or in any combination form the subject matter of the invention, regardless of their summary in the claims or their back references.

Show it:

1 the construction of a conventional multistage fixed bed reactor,

2 the structure of a reactor according to the invention, and

3a and 3b the structure of a used thermal sheet.

1 has already been discussed with reference to the prior art.

2 now shows a reactor according to the invention 20 , Via a supply line 22 is educt, such as methanol, in a distribution chamber 23 brought in. From this distribution chamber 23 branch off a plurality of openings, for example slits, into the reactor 20 to lead. The distribution chamber 23 can be directly on the reactor 20 be attached or even part of the reactor 20 be formed and, for example, by a bulge. However, the distance between the openings and the actual reaction area should always be chosen so that the reaction area is uniformly flown.

At the same time it is also possible in a manner not shown, the reaction medium via nozzles in the reactor 20 contribute. In this case, then the nozzles are to be arranged so that a uniform flow is ensured.

The reaction rooms 25 ₁ to 25 ₆ , are defined by heat transport spaces 24 ₁ to 24 ₇ , which are formed from at least one thermal blanket. The reaction rooms 25 ₁ to 25 ₆ are at least partially filled with catalyst as indicated, on which the reaction medium, such as methanol, can react.

The resulting product stream is passed over the line 26 deducted.

The distance between each two adjacent heat transport spaces 24 _n to 24 _{n + 1} defines a reaction space 25 _m with the width d1. The arrangement follows in such a way that the reaction medium first the reaction spaces 25 ₁ to 25 _{6 flows} vertically from top to bottom and in the lower adiabatic area 21 the reaction spaces not through individual heat transport spaces 24 ₁ to 24 ₇ are separated from each other. In this area 21 If the reaction is adiabatic, there is no heat removal or heat input. In the area of the heat transport spaces 24 ₁ to 24 ₇ can be assumed to be an approximately isothermal reaction regime become. The heat exchanger plates 24 ₁ to 24 ₇ also each have at least one inlet and one outlet, not shown. In addition, it is also possible in a manner not shown to already provide catalyst above the heat transport spaces and thus to expand the reaction spaces.

The catalyst is located on at least one holding device 27 , such as a suitable grid. This holding device 27 can via a sampling device 28 be displaced or dissolved so that the catalyst falls down and at the bottom of the reactor 20 can be easily removed.

3a shows an xy view on a thermo sheet 30 over the surface of a sheet, which forms one side of the thermal sheet. The points 31 ₁ to 31 ₉ represent the so-called welding points, with which the sheet is connected to the sheet metal, not shown, on the opposite side by an additional spot welding. The points 31 ₁ to 31 ₃ , 31 ₄ to 31 ₆ and 31 ₇ to 31 ₉ are each on a straight line, wherein alternately the points of each second line lie again on a straight line in the other dimension. The straight lines run parallel to one another and have the spacing d5.

By the thermal sheet is welded together not only at the edges of two superimposed sheets, but additional welding points 31 ₁ to 31 ₉ can be found in the xz view by a thermo sheet in 3b shown sectional view. Between the individual spot welds 31 ₁ to 31 ₉ channels form 32 ₁ and 32 ₂ , which are usually produced by in a pressure deformation, particularly preferably by a hydroforming. The diameter of such a channel 32 ₁ or 32 ₂ d2 describes the distance between the two sheets 30a and 30b at the maximum channel formation, while the diameter d4 the thickness of the weld point 31 ₁ to 31 ₉ designated. The distance between two welds 31 ₁ to 31 ₉ , which is exactly the distance of two welds 31 ₁ to 31 ₉ on a straight corresponds to d3. Preferably: d3>d2> d4.

embodiments

example 1

Example 1 shows the differences in a reactor design comparing a prior art reactor as in 1 is shown and the reactor according to the invention, which is designed annular in the horizontal. The data for the reactor according to the prior art are in each case 100%, while the reactor according to the invention is indicated in relation to it. Table 1: Comparison of the geometric dimensions of a reactor according to the prior art and the reactor according to the invention. parameter State of the art Example of inventive reactor Catalyst weight (t) 150 150 Total catalyst bed height (m) 100% 100% Total temperature increase (K) 100% about 15% Heat dissipation (MW) 100% 100% Reactor diameter (m) 100% about 60% Reactor length (m) 100% (with construction) 90% Reactor Weight (empty) (t) 100% approx. 50% Volume d. Catalyst (m ³ ) 100% 100% Volume d. Reactor (m ³ ) 100% (without construction) about 40% V _catalyst / V _reactor 100% about 250%

The cross-sectional area in the horizontal can be filled round but of course in any other form. It is crucial that the shape of the reactor allows a good distribution of the reaction medium and easy handling of the catalyst.

It is clear that the dimensions of the reactor according to the invention are significantly reduced, since the local heat removal on the very large heat exchangers can ultimately be dispensed with. The ratio of catalyst to reactor volume is almost three times higher. The space-time yield in the reactor according to the invention is thus drastically improved.

Example 2

Example 2 shows by way of running with Matlab ^® simulation that propylene selectivity in the reactor according to the invention by an improved reaction can be increased closer to an isothermal operation, at least 2%. This is correlated with the fact that there is a much lower temperature difference over the total flow distance of the reaction medium. The data for the reactor according to the prior art are in each case 100%, while the reactor according to the invention is indicated in relation to it. Table 2: Comparison of the geometric dimensions of a reactor according to the prior art and the reactor according to the invention. parameter State of the art inventive reactor Catalyst weight (t) 150 150 Total catalyst bed height (m) 100% 100% Total temperature increase (K) 100% about 15% Heat dissipation (MW) 100% 100% Pressure drop across the reactor 100% about 70% Pressure of the reaction mixture at the outlet (bar) 100% 100% Temperature of the reaction mixture at the outlet (° C) 480 ° C 480 ° C Propylene selectivity (mol C%) 65 > 67 Table 3 shows the yield of propylene as a function of a temperature deviation from the ideal reaction temperature. Average temperature deviation to the optimum reaction temperature (K) 15 10 5 2.5 0 Propylene selectivity (mol C%) 65 67 68 68.5 69

Conventional reactor systems show a deviation of about 15 K and thus a propylene yield of 65 mol C%. The new reactor system will be in the range 10 to 0 K, preferably in the range 2.5 to 0 K for the average temperature deviation to the optimum reaction temperature. The propylene yield is thus significantly increased.

LIST OF REFERENCE NUMBERS

10

 Reactor according to the prior art

111-116

 fixed bed

121-126

 heat exchangers

13, 131-136

 Methanol supply line

14

 Product withdrawal line

20

 inventive reactor

21

 adiabatic area

22

 supply

23

 distribution chamber

241-247

 Heat transport space

24D

 Through opening

251-256

 reaction chamber

26

 derivation

27

 holder

28

 removal device

30

 thermal plate

30a, 30b

sheet

311-319

 WeldingSpot

321, 322

 Heat transport channel

QUOTES INCLUDE IN THE DESCRIPTION

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

Cited patent literature

• DE 10027159 [0005]
• US 2009/0124841 [0005]

Claims (15)

Reactor ( 20 ) for reacting a gaseous and / or liquid reaction medium with at least two reaction spaces at least partially filled with a catalyst (US Pat. 25 ₁ - 25 ₆ ) formed by reacting in the reactor ( 20 ) at least three substantially parallel to each other arranged heat transport spaces ( 24 ₁ - 24 ₇ ) are arranged so the individual reaction spaces ( 25 ₁ - 25 ₆ ) at least partially separate from each other, wherein the heat transport spaces ( 24 ₁ - 24 ₇ ) by at least one thermal plate ( 30 ), each thermo plate ( 30 ) of two sheets ( 30a . 30b ), which are interconnected at the edges and a plurality of further positions above the surface, characterized in that in operation the horizontal extent of the reactor ( 20 ) is greater than its vertical extent in at least one axis and the inlet ( 22 ) as well as the outlet ( 27 ) are provided for the reaction medium so that the reactor ( 20 ) is flowed through vertically by the reaction medium. Reactor ( 20 ) According to claim 1, characterized in that the reaction spaces ( 25 ₁ - 25 ₆ ) vertically over the extent of the heat transport spaces ( 24 ₁ - 24 ₇ ) extend out. Reactor ( 20 ) according to claim 1 or 2, characterized in that the further positions with which the sheets 30a . 30b lie on straight lines, with the distance between the individual positions ( 31 ₁ - 31 ₉ ) always have the same distance d3 to each other on a straight line and the straight lines always have the same distance d5 from each other. Reactor ( 20 ) according to one of the preceding claims, characterized in that the thermal sheets ( 30 ) between the positions ( 31 ₁ - 31 ₉ ) pillow-like channels ( 32 ₁ , 32 ₂ ), in which the maximum distance of the two sheets ( 30a . 30b ) have the distance d2 to each other, and that the distance d1 between two adjacent thermal sheets ( 25 ) is greater than d2 and that the distance d1 is less than 100 times the distance d2. Reactor ( 20 ) according to claim 4, characterized in that the distance d1 is between 1.5 · d2 and 10 · d2 and / or the distance d3 is greater than the distance d2. Reactor ( 20 ) according to one of the preceding claims, characterized in that a removal device ( 28 ) is provided for the catalyst. Reactor ( 20 ) according to one of the preceding claims, characterized in that the heat transport spaces ( 24 ₁ - 24 ₇ ) are designed to guide a molten salt and wherein the heat transport spaces ( 24 ₁ - 24 ₇ ) are arranged so that the thermal sheets ( 30 ) when the device is shut down by gravity. Reactor ( 20 ) according to any one of the preceding claims, characterized in that the reaction spaces ( 25 ₁ - 25 ₆ ) are to be filled with a catalyst bed, wherein the reactor ( 20 ) per m ^{3 of} catalyst bed at least one thermal plate ( 30 ) and / or per m ^{3 of} catalyst bed at least 10 m ² cooling surface. Reactor ( 20 ) according to one of the preceding claims, characterized in that in at least one heat transfer space an additional passage opening ( 24 _D ) from a reaction space ( 25 ₁ - 25 ₇ ) is provided to another. Reactor ( 20 ) according to one of the preceding claims, characterized in that the reactor ( 20 ) a gas distribution device ( 23 ), through which the reaction medium uniformly on all reaction spaces ( 25 ₁ - 25 ₆ ) is distributed. A process for reacting a gaseous and / or liquid reaction medium having at least two at least partially filled with a catalyst reaction spaces, wherein the reaction medium flows through the individual reaction chambers, wherein the reaction spaces are formed by at least three substantially parallel heat transfer spaces and wherein a heat transport medium through the Heat transport spaces flows, which are each formed by at least one thermal blanket, wherein each thermal blanket consists of two sheets, which are connected at the edges and a plurality of other positions above the surface, characterized in that the reaction medium flows through the reactor vertically, wherein the horizontal expansion of the reactor in at least one axis is greater than its vertical extent. A method according to claim 11, characterized in that the heat transport medium is conducted in cocurrent or in countercurrent or in crossflow to the reaction medium. A method according to claim 11, characterized in that the heat transfer medium is liquid at any position in the thermal plate or evaporated in the thermal plate. Method according to one of claims 11 to 13, characterized in that the individual reaction spaces are operated partially adiabatic. Method according to one of claims 11 to 14, characterized in that oxygenates are at least partially reacted to propylene.

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