DE102016204840A1 - Temperature-optimized device for reactions of gaseous media and method for the thermal homogenization of a reaction region - Google Patents

Abstract

The invention relates to a device (1) for thermal reactions of fluids, in particular gaseous media on solids, with an inlet (11) for process fluid (PG); an outlet (12) for the process fluid; a reaction area (13) with the solids extending between inlet and outlet in a longitudinal direction (Lz); a wall (16) enclosing or delimiting the reaction area (13); said apparatus (1) comprising internal heat distribution means (20; 20a; 20b) disposed in the reaction zone (13) which extends more longitudinally than transversely and is adapted to heat energy from a heat emitting zone (13out) of said reaction zone to a heat receiving zone Zone (13in) of the reaction region in the longitudinal direction in the reaction region (13) between inlet (11) and outlet (12) to distribute. The invention further relates to a method for the thermal homogenization of a reaction region (13) of such a device through which process fluid (PG) flows, and to a logic unit (30) designed to carry out the method.

Description

The invention relates to a device for reactions of gaseous media on solids and a method for the thermal homogenization of a reaction region of the device. The device has an inlet and an outlet for process fluid. Between the inlet and outlet extends in the longitudinal direction of a reaction region in which the solids are arranged, and which is bounded or bounded by a wall. In particular, reformer tubes are concerned, which are heated from the outside by means of firing, and in which pressure conditions in the range of e.g. 2 to 60 bar and temperatures above 800 or 900 ° C prevail.

Reaction areas such as e.g. Catalyst beds in reaction tubes in some cases must be externally supplied with thermal energy, especially in endothermic reactions, e.g. in reformer tubes. If the heat energy is introduced via the wall, it is not possible in many cases in a simple manner to enter different amounts of energy in the axial direction. However, this would be advantageous, in particular with regard to a cold inlet region or beginning of the reaction tube, or a process temperature rising with increasing run length. This problem arises e.g. with external energy input by firing.

Also, the forwarding of heat energy within the reaction region is in many cases associated with difficulties, especially in highly insulating solids or catalyst materials. In stationary fixed beds, this problem is particularly noticeable, especially if no heating devices can or should be provided inside the reaction area. Especially in installed in remote areas reformer tubes is trying to dispense with electric heaters and to accomplish the heat input solely by means of natural gas or waste gases.

A strong temperature imbalance, especially in the axial direction, leads to the fact that the reaction range is not utilized efficiently or that side reactions occur, e.g. because the temperature of large areas is too low or too high. All this brings with it further disadvantages, e.g. greater pressure loss due to longer reaction areas or fixed beds.

The object of the invention is to provide a device and a method with the features described above are available, whereby the utilization of the reaction region can be improved.

This object is achieved by a device for thermal, in particular endothermic reactions of fluids, in particular gaseous media to solids, in particular adapted to receive energy from an external heat source, such as energy by firing, with an inlet for process fluid, in particular process gas; an outlet for the process fluid; a reaction area with the solids extending between inlet and outlet in a longitudinal direction; a wall enclosing or delimiting the reaction area, in particular a thermal bridge for absorbing external thermal energy and for transferring the heat energy to the process fluid or into the reaction area, in particular in the radial direction orthogonal to the longitudinal direction; the device comprising an internal heat distribution device arranged in the reaction region, in particular for passively induced heat transfer, which extends more longitudinally than transversely and is arranged to transfer heat energy from a second temperature heat emitting zone of the reaction zone to a first temperature; Heat-absorbing zone of the reaction region in the longitudinal direction in the reaction region between the inlet and outlet to distribute, in particular against the flow direction of the process fluid.

As a result, a comparatively homogeneous temperature distribution in the reaction region can be ensured. In particular, the temperature in the region of the inlet can be increased. Heat energy can be conducted into a heating zone, whereby the heating time required to reach a desired temperature can be shortened. Last but not least, the more homogeneous temperature distribution can also enable a larger process fluid volume flow.

The distribution of the heat energy can be self-regulating depending on the prevailing temperature differences, in particular substantially in one direction, especially in the longitudinal direction. The heat transfer takes place in particular by convection.

The internal heat source can be firmly fixed or anchored in the reaction region, and be positioned or held for example by means of spacers centric to the wall.

The device may be tubular or tubular. The device may be formed as a reaction tube or include this.

As a process fluid is primarily a gas or gas mixture to understand, but which may also have liquid ingredients. According to a variant, the process fluid may also be in the form of a liquid be understood, in particular with gaseous components. The term process fluid includes in particular all variants or mixtures of gaseous with liquid substances.

At the inlet, the process fluid is at a first temperature, and at the outlet, the process fluid is at a second temperature, wherein in particular in endothermic reactions in reformer tubes, the second temperature is significantly higher than the first temperature. The first temperature is e.g. 500 to 550 ° C, and the second temperature is e.g. 750 to 800 ° C. However, the temperature conditions may also differ, in particular, they can reverse.

In a second warmer zone of the reaction region, heat energy can be absorbed and delivered to a first colder zone of the reaction zone. This makes it possible to reduce temperature gradients in the reaction region, in particular in the longitudinal direction. As a result, a shift of energy can take place, in endothermic reactions, in particular in the direction of the inlet.

The energy of the external heat source may be, at least partially, reaction energy required for the reaction (s) in the reaction region. The reaction region may comprise at least one fixed bed. Optionally, another type of bed or bedding may be provided.

According to one embodiment, the internal heat distribution device for axial internal heat transport in the longitudinal direction of the heat-emitting zone is arranged in the heat-receiving zone, in particular against the flow direction of the process fluid, in particular along a longitudinal axis of the device. As a result, heat energy can be transported back, regardless of flow conditions in the reaction area. In this case, the internal heat distribution device for axial internal heat transport in the longitudinal direction can be set up from a first end of the internal heat distribution device to a second end of the internal heat distribution device, in particular counter to the flow direction of the process fluid, in particular along a longitudinal axis of the device.

In this case, the ends of the heat distribution device can each be arranged in the heat-emitting or heat-absorbing zone. This allows a good efficiency in the distribution of heat energy with respect to a specific temperature difference in the reaction area.

The internal heat distribution device can be set up for internal heat transport transversely to the heat transfer induced by the external heat source in the radial direction or orthogonal to the longitudinal direction.

The internal heat distribution device may be arranged for heat transfer by displacement of a working fluid of the internal heat distribution device, in particular in the longitudinal direction of a second temperature present at the end of the internal heat distribution device or a heat-emitting zone of the reaction region to a present at a first temperature end of the internal heat spreader or a heat-accepting zone of the reaction area.

According to one embodiment, the heat distribution device extends from the inlet or from the beginning of the reaction region or from the heat-receiving zone to the outlet or to one end of the reaction zone or to the heat-emitting zone or at least 80% or 90% of this route. This allows efficient heat absorption and delivery, especially with large temperature differences between the beginning and the end. The beginning or the end can also be defined by a range of 5% or 10 to 20% of the length of the reaction region.

According to one exemplary embodiment, the internal heat distribution device has a working fluid in both the liquid and the gas phase and is designed to circulate the working fluid including phase changes, in particular in the longitudinal direction between two ends of the heat distribution device. As a result, heat transfer based on a cycle or at least axial mass transfer can take place within the reaction region. The mass transfer can be autonomous, based solely on local heat from the outside.

The circuit guide can correspond to a cyclic process with phase change, in particular liquid - gaseous - liquid. The circuit guidance can be passive, in particular based on or supported by the highest possible temperature gradient within the internal heat distribution device, which can be increased by a clever positioning of heat conducting elements.

A working fluid of the internal heat spreader may be e.g. be provided in the form of water or ammonia, or by sodium, potassium, zinc or other substances with respect to heat capacity or heat transport comparable properties.

Advantageously, the internal heat distribution device has at least one heat pipe, in particular a heat pipe or a thermosyphon or is designed as a heat pipe. It has been shown that a good distribution effect can be achieved by means of heat pipes.

According to one embodiment, the internal heat distribution device is arranged centrally in the device. This allows a very homogeneous heat distribution. The heat distribution device can fill the coldest zone of the reaction area.

In one embodiment, the reaction area extends concentrically around the internal heat spreader. As a result, a homogeneous heat distribution can be made possible. In this case, the reaction region can be formed annular cylindrical.

According to one embodiment, the heat distribution device extends in the longitudinal direction parallel to the wall. This allows a heat transfer to the reaction region advantageous interaction of the heat distribution device with the wall, in particular with external heat input, for. by firing.

According to one exemplary embodiment, the heat distribution device is arranged at least at the beginning of the reaction region and extends at least in sections along the reaction region or along the wall, in particular at least along 50% of the reaction region. As a result, heat can be introduced at the beginning from the inside into the reaction region, in particular in order to counteract a supercooled initial region. This also improves the efficiency of the reaction area.

Advantageously, the internal heat distribution device extends at least 75 to 85%, preferably in the longitudinal direction completely along the reaction region. A longitudinally completely along the reaction region extending internal heat distribution device provides a particularly efficient heat transfer in the longitudinal direction and counter to the longitudinal direction.

In this case, the internal heat distribution device can extend along the wall or thermal bridge.

According to one exemplary embodiment, the internal heat distribution device has, in particular on an outer lateral surface at at least one longitudinal position, at least one heat conducting element which extends radially in the direction of the wall, in particular a plurality of heat conducting elements oriented parallel to one another. This can improve the local energy intake. The efficiency of the heat distribution device can be improved.

The respective thermal element can improve the energy absorption and increase the homogenizing effect of the internal heat distribution device. The respective heating element can e.g. as a fin, fin, step, elevation, or more generally as an element of enlarged, e.g. be formed cylindrical surface of the internal heat distribution device protruding surface.

According to one exemplary embodiment, at least one heat-conducting element of the internal heat-distributing device is positioned in a longitudinal position corresponding to the beginning of the reaction region, in particular in a heat-absorbing zone. As a result, heat energy can be delivered from the heat distribution device targeted at the beginning of the reaction area. This arrangement provides advantages especially in reformer tubes. For example, the heating-up length can be noticeably shortened as a result.

According to one exemplary embodiment, at least one heat-conducting element of the internal heat-distributing device is positioned in a longitudinal position corresponding to the end of the reaction region, in particular in a heat-emitting zone. As a result, the heat transfer can be locally concentrated. The heat distribution device can absorb or release increased heat by means of the locally arranged heat-conducting elements at specific longitudinal positions of the reaction region. In addition, the way in which heat is introduced into the reaction zone can be influenced, be it geometrically or quantitatively. The heat-conducting elements are preferably arranged circumferentially around the heat-distributing device, be it as ring elements, be it continuously circulating, e.g. every 30 ° circumferential angle in the circumferential direction. This allows a heat absorption or release in a particularly homogeneous manner.

Heat-conducting elements positioned at the beginning of the reaction area and / or at a first end of the internal heat distribution device may be arranged, geometrically formed and / or dimensioned symmetrically to heat-conducting elements positioned at the end of the reaction area and / or at a second end of the internal heat-distributing device. This makes it possible to operate the device in the opposite direction of flow, e.g. from bottom to top instead of top to bottom. The heat transfer or a flow profile can then form unchanged even in the opposite direction of flow.

According to one exemplary embodiment, at least one heat-conducting element of the internal heat distribution device is aligned in the longitudinal direction or in the flow direction. As a result, passing gas can be heated particularly effectively and no flow obstacles are created.

The internal heat distribution device may each have a plurality of heat-conducting elements at two locations, in particular at one end in each case. It has been shown that the arrangement of the heat-conducting elements in the maximum axial distance from each other in the device favors a high efficiency of the axial heat transport in the reaction region. A temperature gradient within the internal heat spreader can thereby be maximized. This results in a heat pipe or a thermosyphon with the result that at a given working medium at one end a comparatively large amount of energy can be absorbed and can be discharged again at the other end.

For a vertically disposed internal heat spreader, the at least one heat conducting element may then be e.g. be arranged at the lower end and be aligned in the longitudinal direction. This allows not only an efficient heat transfer but also the homogeneous distribution of solid particles when filling the reaction area or reaction tube.

According to one exemplary embodiment, at least one heat-conducting element of the internal heat-distributing device is aligned in the radial direction orthogonal to the longitudinal direction or in the flow direction. As a result, the reaction region in the flow direction can be at least partially delimited, e.g. of inert particles. This orientation may also have advantages in an arrangement of the heat-conducting elements upstream of the reaction region.

Optionally, as high a temperature gradient as possible between the ends of the heat source, e.g. also be effected by means of at least one heating device. The passive heat transfer of the internal heat distribution device can be enhanced by a heater by actively or in a controlled or regulated manner heat energy is supplied locally at a certain position (in particular at one end) of the internal heat distribution device.

The internal heat distribution device may comprise at least one heating device for local, local supply of internal heat energy into the internal heat distribution device and / or into the reaction region, wherein the heating device is preferably arranged at one end of the heat source. A heat source arranged at one end can cause a temperature gradient within the heat source, in particular a temperature gradient in the longitudinal direction. This can improve the efficiency of the heat spreader.

A heating device of the internal heat distribution device may be arranged in the region of the end of the reaction region. The heating device may be arranged in the flow direction of the process fluid behind the end or downstream of the end of the reaction region. This allows a local heat input without affecting the temperature distribution in the reaction area.

According to one embodiment, the device comprises in the longitudinal direction or in the flow direction before or after the reaction region, in particular behind one end of the internal heat distribution device or in the flow direction behind a heat-emitting zone of the reaction region inert material, in particular a bed of inert particles. As a result, the heat absorption in the heat distribution device can be influenced, in particular if a heat-receiving zone or an output-side end of the heat distribution device is surrounded by inert particles. The inert particles may e.g. have a particularly high heat capacity.

The inert material may be in the flow direction of the process fluid e.g. be arranged behind / downstream of the end of the reaction region, in particular surrounding at least one heat-conducting element. By means of the inert material it can be ensured that no unwanted temperature changes take place in the reaction area, in particular no temperature drop. The heat-emitting zone may be formed or filled by inert material.

It may also be advantageous if a heat-emitting zone or an input-side end of the heat distribution device is arranged above the reaction region and optionally also surrounded by inert particles. This makes it possible, for example, to introduce thermal energy into the process gas before the process gas is introduced into the reaction zone.

According to one exemplary embodiment, the device comprises at least one in particular insulating element insulating the internal heat distribution device, which extends in the longitudinal direction in sections along the internal heat distribution device and along the reaction region, in particular a cladding tube surrounding the internal heat distribution device in a middle section. As a result, the heat output can be influenced locally. In particular, heat energy can be used in one middle area are retained. The heat transport up to a beginning of the reaction area can be made even more effective.

Between heat-conducting elements, which are arranged at different longitudinal positions, can e.g. also be arranged a cladding tube on the internal heat distribution device. By means of the cladding tube, it is possible to influence the geometry of the reaction region or flow conditions in the region of a lateral surface of the internal heat distribution device or of the cladding tube. Furthermore, a heat transfer from a longitudinal section between the heat-conducting elements to the reaction area can also be influenced, in particular prevented. This can increase the efficiency of heat exchange between the ends of the internal heat spreader, especially due to a higher temperature gradient within the heat source. The cladding tube may e.g. consist of an insulating material, especially ceramic. The cladding tube may e.g. be arranged adjacent to one or more heat-conducting elements. The cladding tube may e.g. be arranged between heat conducting elements, which are each arranged at one of the two ends of the heat distribution device. The cladding tube may e.g. also be arranged adjacent to a heater.

According to one exemplary embodiment, the wall is set up for an energy supply, in particular firing, by at least one external heat source, wherein the reaction region comprises at least one catalyst bed. The device may comprise the at least one external heat source. The external heat source may cause an increasing temperature in the reaction region with increasing run length and a certain temperature gradient between inlet and outlet, wherein the temperature gradient can be lowered by means of the heat distribution device.

The device may be formed in the region of the wall and / or along the reaction region at least partially tubular. This allows a homogeneous heat distribution or a symmetrical flow profile. The wall or thermal bridge can be formed by a tube wall, in particular a cylindrical tube wall. The entire device may be formed as a reaction tube or include this. The device may comprise a reformer tube, wherein the wall is a part of the reformer tube.

The aforementioned object is also achieved by a method for the thermal homogenization of a flowed through by process fluid reaction region, in particular a reaction region of a device described above, in particular a reaction region in a reformer tube for endothermic reactions of solids with at least one fixed or fluid bed, wherein the process fluid is passed from a present at a first temperature zone of the reaction region to a present at a second temperature not equal to the first temperature zone of the reaction region; wherein at least one disposed in the reaction region internal heat spreader, in particular a passive induced heat transfer heat source is operated so that internal heat energy within the internal heat spreader from the zone of the second temperature to the zone of the first temperature or transported and distributed in an opposite the zones is discharged and thereby the first and second temperature are equalized to each other, in particular transversely to an induced by at least one external heat source radial heat transfer.

The operation of the internal heat spreader may e.g. by adjusting the process fluid volume flow, the amount of externally applied heat energy and / or input temperature of the process fluid. These or other parameters can influence the temperature profile that is set in the process area.

In this case, heat energy or reaction energy can be introduced into the reaction region by means of at least one external heat source, in particular by firing.

According to one embodiment, the internal heat transfer in the internal heat distribution device is caused in at least one heat pipe due to a difference between the first and second temperature, in particular self-regulating by convection in a heat pipe or a thermosyphon. The reaction region can be supplied with process fluid in such a way that a temperature difference arises which causes the internal heat transfer. In this way, the reaction region can be used efficiently, in particular in the case of large volume flows, and the reaction can take place over a maximum run length of the reaction region, in particular under as homogeneous as possible boundary conditions.

In this case, an energy supply, in particular firing by at least one external heat source can be carried out in the reaction area. The external energy supply may cause or contribute to an increasing temperature in the reaction region with increasing run length, so that a certain temperature gradient between the inlet and outlet is established, which can be lowered again by means of the heat distribution device. The Interaction between external heat source and heat spreader can be controlled or regulated.

According to one embodiment, local heat energy is supplied to the internal heat distribution device locally, in particular by means of at least one heat conducting element and / or by means of a heating device at the beginning and / or at the end of the reaction region. The reaction area can be acted upon by process fluid in such a way that a temperature difference with a temperature maximum at one end of the heat distribution device and a temperature minimum at a beginning of the heat distribution device are established. This can cause a strong temperature gradient within the internal heat distribution device.

The aforementioned object is also achieved according to the invention by a logic unit configured to carry out a method described above, wherein a volumetric flow of the process fluid and / or an inlet temperature of the process fluid and / or the amount of locally supplied energy and / or the time or the duration of the energy supply are controlled or regulated, in particular also an energy supply of at least one external heat source. Here, the logic unit may be in communication with corresponding sensors, in particular at least one volume flow sensor, at least one temperature sensor, at least one of the power or energy detecting sensor or at least a chronometer.

A logic unit is not necessarily required to effect thermal homogenization, in particular, the heat spreader may autonomously operate in response to temperature differences. However, the logic unit may improve the interaction between multiple heat sources or also improve the efficiency of a potentially quite passive heat spreader. For this purpose, the logic unit can be in connection with at least one external heat source. In the reaction region, in particular at the beginning and at the end, in each case temperature sensors can be arranged, by means of which the current temperature differences can be detected. There may be a threshold for certain temperature differences, e.g. between the beginning and the end, and the at least one external heat source can be controlled and regulated as a function of the actual temperature difference.

The aforementioned object is also achieved by the use of an internal heat distribution device, in particular a heat pipe, for the thermal homogenization of a process fluid flow through a reaction region of a device for reactions of fluids to solids, in particular in a device described above or in a reformer tube, wherein the heat transport through a temperature difference is caused in the reaction region and by means of a phase change underlying working fluid by convection. This results already mentioned advantages.

Advantageously, the internal heat distribution device is arranged centrally in the reaction region along its longitudinal axis and adapted for heat transport in the longitudinal direction.

Further features and advantages of the invention will become apparent from the description of at least one embodiment with reference to drawings, and from the drawings themselves. It shows

1 in a schematic side view components of a device with heat distribution device according to an embodiment;

2 in a schematic side view components of a device with heat distribution device according to another embodiment;

3 in a schematic side view components of a device with heat distribution device according to another embodiment;

4A a schematic representation of the operation of a heat distribution device when used in a device according to an embodiment;

4B a schematic representation of a temperature profile in the longitudinal direction in a reaction region of a device according to an embodiment;

5A . 5B a schematic representation of the temperature profile of a reaction tube without heat distribution device in direct comparison with the temperature profile in a reaction region of a device according to an embodiment; and

6 a schematic representation of a device according to an embodiment comprising a logic unit, a heater and / or sensors.

For reference numbers that are not explicitly described with respect to a single figure, reference is made to the other figures.

The 1 shows components of a device 1 for reactions of gaseous media on solids, with a reaction tube 10 , especially Reformer tube, with an inlet 11 and an outlet 12 each for process gas PG. The process gas PG is through a reaction area 13 , in particular with catalyst particles or -schüttung passed and absorbs heat or gives off heat, depending on the nature of the reaction. About the reaction area 13 bounding wall or thermal bridge, in particular pipe wall 16 can an externally induced (external) heat flow Qext into the reaction area 13 be initiated. A perforated plate, net or grid 18 can the reaction area 13 limit, down here as shown.

In the reaction area 13 is an internal heat spreader 20 arranged, in particular a heat pipe, namely a so-called heat pipe or a thermosiphon, which extends along a longitudinal axis (dashed line) of the reaction region in the longitudinal direction Lz. A (outer) envelope surface 21 borders the heat distribution device 20 from the reaction area 13 from.

At as far apart longitudinal positions, in particular at the ends of the heat distribution device 20 are each heat-conducting elements 22 arranged, in particular in the radial direction x, y or in an orthogonal to the longitudinal axis extending xy plane radially aligned ribs 22 , or longitudinally oriented ribs 23 ( 2 . 3 ).

In the reaction area 13 or the bed there is a temperature gradient. For example, one end of the reaction area 13 hotter than a start or inflow zone. The heat distribution device 20 is configured to locally absorb and deliver thermal energy, the hotter portion of the reaction area (here the outflow area) of a heat-emitting zone 13out and the cooler portion of the reaction area 13 a heat-absorbing zone 13in equivalent. The heat-conducting facilitate a local heat absorption and release, and also allow influence on the location or the type or direction of heat transfer. The local heat absorption and delivery, in particular at the ends of the heat distribution device 20 is designated by the reference Qint according to an internally generated (internal) heat flow. This local heat flow constitutes an additional heat flow Qsup, which is opposite to the longitudinal direction within the heat distribution device 20 , For better clarity, the additional heat flow Qsup is represented by an external arrow, but it is an internal heat flow within the reaction area 13 , corresponding to an additional induced energy or heat flow Qz in the z-direction, which takes place autonomously without any further energy supply.

In the 1 as well as in the following figures, temperature differences or gradients are represented by hatches of different tightness, wherein a particularly wide hatching indicates a particularly high temperature. The closer the hatching, the cooler the corresponding zone.

The 2 shows a reaction tube 10 with a heat distribution device 20a in which in the longitudinal direction ( 1 ) oriented Wärmeleitelemente 23 are provided. A lower end of the heat spreader 20a is in a pile 14 arranged from inert particles and by means of a grid 18 from the reaction area 13 demarcated. In this arrangement, a heat absorption takes place by the heat distribution device 20a also to a significant extent below the reaction range. However, the heat is completely within the reaction area.

The 3 shows a reaction tube 10 with a heat distribution device 20b in which both in the radial direction aligned heat conducting elements 22 as well as in the longitudinal direction Lz aligned heat conducting elements 23 are provided. A lower end of the heat spreader 20b is in a pile 14 arranged from inert particles and by means of a grid 18 from the reaction area 13 demarcated. The radially oriented heat conducting elements 22 are above the reaction area 13 arranged. In this arrangement, a heat absorption and release also takes place separately from the reaction area, which can increase the efficiency of the axial heat transport.

The 4A shows the operating principle of a heat distribution device 20 when used in one of the 1 . 2 . 3 shown device. A working fluid WF is placed in a heat receiving section 20in the heat distribution device 20 is heated and thus undergoes a phase change, evaporates and rises in the opposite direction, which causes an energy transfer Qz. With increasing height or distance from the heat-absorbing section 20in the energy content of the working fluid WF is reduced, in particular due to energy release in a heat-emitting section 20out to a heat-receiving zone 13in the reaction area 13 ,

The 4B schematically shows a possible temperature profile in the reaction area 13 when using a heat spreader 20 , In a reaction tube 10 without heat distribution device, a comparatively large temperature gradient ΔTz arises in the longitudinal direction. The temperature T is in a heat-emitting zone 13out comparatively high. When using a heat spreader 20 however, the temperature gradient .DELTA.Tz can be reduced, with the result that a desired target temperature T1 can already be achieved at a comparatively short run length z1. A heating zone can be shortened, especially by providing a heat-absorbing zone 13in is arranged overlapping the heating zone.

The 5A . 5B show a temperature profile in a reaction tube 10 without heat distribution device in comparison with a temperature profile in a reaction tube 10 with heat distribution device 20 (Dot-dash line). When using the heat distribution device 20 For example, the run length or heating zone z1 can be significantly shortened until the temperature T1 is reached. The temperature distribution is more homogeneous.

The 6 shows a device 1 for reactions of gaseous media to solids in a schematic representation, wherein in the reaction tube 10 a heat distribution device 20 . 20a ; 20b is arranged, on which sensors, in particular a plurality of temperature sensors 32 . 33 are arranged. Furthermore, further sensors, in particular at least one flow sensor 31 in other places of the device 1 be provided. The sensors 31 . 32 . 33 are connected to a logic unit 30 coupled. Optionally, a heating device 24 be provided, in particular at the output end of the internal heat distribution device, by means of which the internal energy transport Qz can be supported. An energy input by means of the heater 24 may favor or actively influence a phase change of working fluid of the heat spreader, if desired. This makes it possible to regulate energy flows, in particular in phases in which no lasting temperature profile has yet formed in the reaction region, for example when starting up a sorption process or for the first time heating of process gas.

LIST OF REFERENCE NUMBERS

1

 Device for reactions of gaseous media on solids

10

 Reaction tube, in particular reformer tube

11

 inlet

12

 outlet

13

 Reaction area, in particular with catalyst particles or bed

13in

 heat-absorbing zone

13out

 heat-emitting zone

14

 inert particles or inert bed

16

 Wall or thermal bridge, in particular pipe wall

18

 Perforated sheet, mesh, grid

20, 20a, 20b

 internal heat distribution device, in particular heat pipe, namely heat pipe or thermosyphon

20in

 heat-absorbing section

20out

 heat-emitting section

21

 (Outer) envelope surface

22

 Wärmeleitelement, in particular radially arranged rib

23

 Wärmeleitelement, in particular longitudinally arranged rib

24

 Heating device, in particular at the output end of the internal heat distribution device

30

 logic unit

31

 Sensor, in particular flow sensor

32, 33

Sensor, in particular temperature sensor

lz

 Longitudinal along the longitudinal axis of the reaction tube or the device or the reaction region

PG

 Process fluid, in particular process gas

WF

 working fluid

Q ext

 Externally generated (external) heat flow

Qint

 Internally generated (internal) heat flow

Qsup

 additional heat flow

Qz

 additional energy or heat flow in z-direction

T

 temperature

T1

 Target temperature for run length z1

ΔTz

 Temperature profile or gradient in the axial direction

x

 Coordinate axis in the radial direction orthogonal to the longitudinal axis

y

 Coordinate axis in the radial direction orthogonal to the longitudinal axis

z

 Location coordinate in the direction of the longitudinal axis

z1

 Run length or heating zone

Claims (15)

Contraption ( 1 ) for thermal reactions of fluids, in particular gaseous media on solids, with - an inlet ( 11 ) for process fluid (PG); - an outlet ( 12 ) for the process fluid; A reaction area extending between inlet and outlet in a longitudinal direction (Lz) ( 13 ) with the solids; - one the reaction area ( 13 ) bounding wall ( 16 ); characterized in that the device ( 1 ) one in the reaction area ( 13 ) arranged internal heat distribution device ( 20 ; 20a ; 20b ), which extends more longitudinally than transversely and is adapted to heat energy from a heat emitting zone (FIG. 13out ) of the reaction area to a heat-receiving zone ( 13in ) of the reaction region in the longitudinal direction in the reaction region ( 13 ) between inlet ( 11 ) and outlet ( 12 ) to distribute. Apparatus according to claim 1, wherein the heat distribution device ( 20 ; 20a ; 20b ) from the inlet ( 11 ) or from the beginning of the reaction zone to the outlet ( 12 ) or to at least one end of the reaction region, or at least 80% or 90% of that distance. Device according to claim 1 or 2, wherein the internal heat distribution device ( 20 ; 20a ; 20b ) has a working fluid (WF) both in the liquid and in the gas phase and is arranged to circulate the working fluid including phase change, in particular in the longitudinal direction between two ends of the heat distribution device, wherein the internal heat distribution device ( 20 ; 20a ; 20b ) preferably has at least one heat pipe or is designed as a heat pipe. Device according to one of the preceding claims, wherein the internal heat distribution device ( 20 ; 20a ; 20b ) centric in the device ( 1 ), and / or wherein the reaction area ( 13 ) concentrically around the internal heat distribution device ( 20 ; 20a ; 20b ), wherein the reaction region ( 13 ) is preferably formed annular cylindrical, and / or wherein the heat distribution device ( 20 ; 20a ; 20b ) in the longitudinal direction parallel to the wall ( 16 ). Device according to one of the preceding claims, wherein the heat distribution device ( 20 ; 20a ; 20b ) is arranged at least at the beginning of the reaction region and extends at least in sections along the reaction region, in particular at least along 50% of the reaction region, preferably at least 75 to 85%, more preferably in the longitudinal direction completely along the reaction region. Device according to one of the preceding claims, wherein the internal heat distribution device ( 20 ; 20a ; 20b ) at least one longitudinal position at least one heat conducting element ( 22 . 23 ), which extends radially in the direction of the wall ( 16 ). Device according to one of the preceding claims, wherein at least one heat-conducting element ( 22 . 23 ) of the internal heat distribution device ( 20 ; 20a ; 20b ) is positioned in a longitudinal position corresponding to the beginning or the end of the reaction region, in particular in the heat-absorbing zone ( 13in ) or in the heat-emitting zone ( 13out ). Device according to one of the preceding claims, wherein at least one heat-conducting element ( 23 ) of the internal heat distribution device ( 20 ; 20a ; 20b ) is aligned in the longitudinal direction, and / or wherein at least one heat-conducting element of the internal heat distribution device ( 20 ; 20a ; 20b ) in the radial direction ( 22 ) is aligned orthogonal to the longitudinal direction. Device according to one of the preceding claims, wherein the device ( 1 ) in the longitudinal direction in front of or behind the reaction region ( 13 ) inert material ( 14 ), and / or wherein the device ( 1 ) at least one of the internal heat distribution device ( 20 ; 20a ; 20b ) insulating element, which in the longitudinal direction in sections along the internal heat distribution device ( 20 ; 20a ; 20b ) and along the reaction area. Device according to one of the preceding claims, wherein the wall ( 16 ) is arranged for an energy supply, in particular firing by at least one external heat source (Qext), and wherein the reaction area ( 13 ) comprises at least one catalyst bed. Method for thermally homogenizing a reaction area through which process fluid (PG) flows (US Pat. 13 ) a device ( 1 ) for reactions of fluids with solids, in particular a reaction range of a device ( 1 ) according to any one of the preceding claims, wherein process fluid is from a zone (1) at a first temperature ( 13in ) of the reaction area to a second temperature zone ( 13out ) is passed the reaction region; characterized in that at least one in the reaction area ( 13 ) arranged internal heat distribution device ( 20 ; 20a ; 20b ) is operated such that internal heat energy within the internal heat distribution device from the zone of the second temperature ( 13out ) to the zone of the first temperature ( 13in ) and in one of the zones ( 13in . 13out ) and thereby equalize the first and second temperatures. Method according to the preceding claim, wherein an internal heat transfer in the internal heat distribution device ( 20 ; 20a ; 20b ) is caused in at least one heat pipe due to a difference between the first and second temperatures, and / or wherein in the reaction region ( 13 ) an energy supply, in particular firing by at least one external heat source (Qext) takes place. Method according to one of the preceding method claims, wherein the internal heat distribution device ( 20 ; 20a ; 20b ) locally localized heat energy is supplied, in particular by means of at least one heat conducting element ( 22 . 23 ) and / or by means of a heating device ( 24 ) at the beginning and / or at the end of the reaction area ( 13 ). Logic unit ( 30 ) arranged for carrying out a method according to one of the preceding method claims, wherein a volume flow of the process fluid (PG) and / or an inlet temperature of the process fluid and / or the amount of locally supplied energy and / or the time or the duration of the energy supply are controlled or regulated. Using an internally in a reaction area ( 13 ) arranged heat distribution device ( 20 ; 20a ; 20b ), in particular a heat pipe, for the thermal homogenization of the reaction area through which the process fluid (PG) flows (US Pat. 13 ) a device ( 1 ) for reactions of fluids on solids, in particular in a device ( 1 ) according to any one of the preceding claims, wherein the heat transfer by a temperature difference in the reaction region ( 13 ) is caused by means of a phase change underlying working fluid (WF) by convection.

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