DE102012220930A1 - Fixed bed reactor useful for carrying out catalytic gas-phase reactions, comprises bundle of vertical heat exchanger tubes, catalyst chamber for accommodating catalyst bed, reactor jacket, upper and lower reactor head, and filling device - Google Patents

Abstract

Fixed bed reactor (1) for carrying out catalytic gas-phase reactions, comprises a bundle (9) of vertical heat exchanger tubes whose lower and upper tube ends are respectively connected to at least one heat carrier distributor (28) or heat carrier collector, a catalyst chamber (49) for accommodating a catalyst bed (8), a reactor jacket which encloses the bundle of the heat exchanger tubes and the catalyst chamber, an upper- and lower reactor head which span the upper- and lower tube ends of the heat exchanger tubes, and a filling device for filling the catalyst chamber with a catalyst material. Fixed bed reactor (1) for carrying out catalytic gas-phase reactions, comprises (a) a bundle (9) of vertical heat exchanger tubes whose lower- and upper tube ends are respectively connected to at least one heat carrier distributor (28) or heat carrier collector, (b) a catalyst chamber (49) for accommodating a catalyst bed (8) which abuts outer sides of the heat exchanger tubes, and is passed with a reaction gas during the operating condition of the fixed bed reactor, (c) a reactor jacket which encloses the bundle of the heat exchanger tubes and the catalyst chamber, (d) an upper- and lower reactor head which span the upper- and lower tube ends of the heat exchanger tubes and respectively the heat carrier distributor or the heat carrier collector, exhibit supply- and discharge pipes for feed- and product gas and/or the heat carrier, and are respectively tightly connected to the reactor jacket, and (e) a filling device for filling the catalyst chamber with a catalyst material, which is arranged above the catalyst chamber, and exhibits at least one catalyst distributor which is arranged outside the bundle of the heat exchanger tubes. The catalyst chamber is horizontally limited by a catalyst holder which is designed for horizontally holding the catalyst bed, and is limited vertically downwards by a catalyst support which is designed for vertically supporting the catalyst bed, and extends up to a predetermined height such that a dead space is formed between upper limit of the catalyst chamber and the upper tube ends of the heat exchanger tubes. Several filling tubes which with their upper tube ends open respectively in the catalyst distributor, and extend in the dead space, and with their lower tube ends open in the dead space. The course of all filling tubes is coordinated in the dead space such that, its entire lower tube ends is distributed over entire cross-section of the catalyst chamber.

Description

The invention relates to a fixed bed reactor for carrying out catalytic gas phase reactions, with a bundle of vertical heat exchange tubes and a catalyst space for receiving a catalyst bed, which bears against the outer sides of the heat exchange tubes and flows through reaction gas in the operating state of the fixed bed reactor.

Catalytic gas phase reactions are generally carried out in fixed bed reactors. Of particular interest are fixed bed reactors with a reaction space or a catalyst bed located therein, which is flowed through radially by reaction gas. With this design, it is possible to create a large flow area at low pressure loss. In the arrangement of heat exchange elements, for. B. in the form of heat exchange tubes, an isothermal operation is still possible.

An important issue in all fixed bed reactors is the filling of the reaction chambers with mostly granular catalyst. The known filling methods are adapted to the respective specific constructions and to the properties of the catalyst used. The goal of any process is the uniform distribution of the catalyst over the flow cross section as a prerequisite for optimal reaction results.

In a radially flowed fixed bed reactor after the US 4,321,234 with homogeneously distributed over the fixed bed cross-section heat exchange tubes, the catalyst is filled through a simple nozzle in the reactor hood in the reactor. This is considered sufficient for a normal particle size catalyst. In a poorly flowable catalyst or in a non-homogeneous arrangement of the heat exchange tubes, however, a uniform distribution of the catalyst is not guaranteed.

At one in the US Pat. No. 7,353,847 B2 In the reactor of this type, the interspaces between the tubes are gradually filled from bottom to top with a granular solid, preferably a catalyst material. In this method, a rigid, vertical column section is first provided of sufficient size to accommodate an operator. This operator stands on a standing surface fastened to the column section and fills the filling space with a particulate solid with a preferably flexible supply line. The filling process is interrupted before the granule surface reaches the upper edge of the column section. Now a second column section of the same kind is placed on the first column section, the base area is converted into the second column section and fastened thereto, and the filling process is continued. The aforementioned steps are repeated until a desired filling level is reached. The container can be an axial, radial, annular, transverse or section-flowed fixed bed reactor. The filling space may contain internals, such as heat exchange tubes, associated supports, distributors or baffles. The stacking of column sections is cumbersome and time consuming.

A method and apparatus of another type for filling catalyst into the reaction space of a fixed bed reactor through which a heat exchange tube bundle passes is disclosed in US Pat US Pat. No. 6,467,513 B1 described. In this case, the catalyst is fed into the reactor through a flexible tube, which is equipped in its interior with fall arrestors that absorb the falling energy of the falling catalyst particles and provide such fall distances that the catalyst does not break when dropped. After filling the catalyst, the catalyst is fluidized. The flexible filling hose has a diameter such that it can not be routed into the interior of a bundle of heat exchange tubes as a rule. Its end can only be conducted next to the bundle. From this point, a bulk cone forms, which is subsequently made uniform by a fluidizing device over the bundle cross-section.

At the in US Pat. No. 6,467,513 B1 Example given fluidization times of 5 to 15 minutes there is a risk of segregation. Since a cycle, consisting of a filling process and a subsequent fluidization, is carried out several times, the fluidization device must be dimensioned sufficiently large so that fluidization over the entire height of the catalyst bed is guaranteed even in the last cycle. Furthermore, the reactor must have a height reserve in the area of the bed surface, since the catalyst bed is in operation. This process is time consuming and costly.

In fixed bed reactors without internals, the distribution devices no longer have to take account of these obstacles which disturb the distribution. Mostly branched distribution systems are used.

For such a reactor type represents the US 4,277,205 a method for improved distribution of the catalyst over the cross section of a reaction space or a catalyst bed before. In this case, solid particles first flow through a feed device into a centrally located trough. A gas flows from below through an am Bottom of the tub located gas-permeable bottom and fluidized so located in the tub solid particles that are discharged in this state in the circumference of the tub mounted distribution lines. The manifolds have different lengths and lead radially away from the trough.

A uniform distribution over the cross section of the reaction space is achieved by a rotation of the tub and the connected distribution lines. This distributor device is adapted for filling cylindrical containers without internals. If fittings are in the form of e.g. Heat exchange tubes present, so a rotation is not possible. In addition, the construction due to the rotation requires a certain amount of space above the center of the reaction space and it is mechanically vulnerable because of the moving parts.

In particular, a number of publications are concerned with reducing the rate of fall in such fixed bed reactors to prevent breakage of catalyst particles by impact during the filling process. Such a method is eg in the DE 196 34 455 A1 described. In this case, the catalyst is fed through a central tube and distributed uniformly and gently in the reactor by means of a rotating distributor device with several distributor heads arranged in a star shape. The special feature lies in the arrangement of the distribution device at the lower end of a height-adjustable telescopic tube. The distribution heads are thus always close to the surface of the catalyst bed and the height of fall of the catalyst particles is always low. The distributor tool can be fixed to a moving platform on which an operator stands, which manually or mechanically turns the distributor tool and can change the bulk cone of the individual distributor heads. The filling process is particularly adapted to mechanically sensitive catalysts and structurally quite complex. The arrangement of the distributor heads only at a central and at a radial position, a uniform distribution over the reactor cross-section of the catalyst is not secured.

In the EP 2 029 463 A1 For example, there is provided a device for filling solid particles into a container having a line with means for damping the falling velocity and a suction device.

Numerous methods and devices for filling reaction tubes of tube bundle reactors are also known. The aim here is to create the same catalyst bed in terms of pressure loss and catalytic effect in each reaction tube. In this sense, the DE 28 49 664 A1 a method for feeding a plurality of tubes in tubular reactors with granular solids, preferably with catalysts, in which two or more varieties of such solids are to be introduced as a mixture into a single tube or a tube group. In this case, a homogenous, independently controllable, material flow is continuously led out of two or more storage containers and introduced via a measuring and control device either offset in time or simultaneously as a mixture via mechanically controllable guide devices via flexible hoses in an individual pipe or in a pipe group. The catalyst is transported with vibrating troughs and belt conveyors.

The US 4,402,643 describes an apparatus for filling granular catalyst into a plurality of reaction tubes. The apparatus comprises a plurality of contiguously arranged storage hoppers for receiving the granular catalyst, a substantially horizontal vibrator below the storage hoppers with discharge openings at the bottom of the vibrator and flexible hoses at the exit of each discharge opening with throttling elements and introduction aids in the reaction tubes at the outlet of each individual tube.

A structurally simple device for filling solid particles in reaction tubes of a tube bundle reactor is in the EP 0 963 785 A1 described. It includes a plurality of adjacent polygonal plates with 1 to 30 holes in each plate. Each hole corresponds to a reaction tube. Each hole has a diameter not larger than 95% of the inner diameter of the reaction tube and not smaller than 1.1 times the largest dimension of a catalyst particle, the polygonal plates also having attachment means for holding the holes on the reaction tubes. These attachment means may be inserts which protrude into the reaction tubes. The filling is carried out so that the catalyst particles are first poured onto the surface of the plates. These are then returned either manually or mechanically into the reaction tubes. When the catalyst bed reaches the top of the plates, the plates are removed and a void is left in the reaction tubes over the catalyst surface, the size of which is dependent on the displaced volume of the insert.

When filling reaction tubes, the horizontal uniformity of the catalyst bed within a reaction tube poses no problem, since a reaction tube is a vertical envelope, which forcibly very narrowly limits the horizontal extent of the catalyst. The task here consists in the uniform filling of all reaction tubes with the highest possible Filling speed. Each reaction tube must be individually controlled and filled.

For the filling of a reaction space between the tubes of a bundle of heat exchange tubes, however, such methods and devices are too complicated and therefore impractical.

The object of the invention is to propose a fixed bed reactor of the type mentioned, which can be filled quickly with a homogeneous and at the same time densely packed catalyst bed.

According to the invention this object is achieved by a fixed bed reactor having the features of claim 1.

The invention makes use of the finding that when filling the catalyst space with catalyst particles on the one hand, the time interval between two impinging on the same place catalyst particles should be sufficiently large so that the impinging catalyst particles do not jam and jam each other, but have sufficient time in one each their own stable position to rotate and slide, and they are thus packed as close as possible, and on the other hand, these intervals should be as evenly as possible to obtain a homogeneous homogeneous packing. With the filling tubes preferably arranged in the form of an ostrich, which extend from a catalyst distributor into the intermediate spaces between the heat exchange tubes into the catalyst-free dead space (ie the unfilled reaction space) between the underside of the upper tube bottom and the top of the catalyst bed to be filled, a stationary filling device can be provided be formed, which can fill in spite of the lack of rotational and vertical movement of catalyst material so that the resulting catalyst bed in the horizontal and vertical direction is homogeneous and tightly packed. Characterized in that the course of all filling tubes in the dead space is coordinated so that the entirety of their lower tube ends is distributed over the entire cross section of the catalyst space, a uniform over the cross section of the catalyst space filling with catalyst material is ensured.

The upper ends of the filling tubes open into a catalyst distributor, so that an uninterrupted uniform influx of catalyst material to each filling tube and thus a uniform over time leakage of catalyst material from the lower ends of the filling tubes - also referred to as trickling - is ensured. The amount of catalyst material that passes through the filling tubes per unit time is determined by the size of the opening cross-section of the filling tubes or the inlet opening at the upper tube ends of the filling tubes. According to the desired trickling speed, the inlet openings or the inner dimensions of the filling tubes can be determined. The catalyst distributor is arranged outside the bundle of heat exchange tubes, so that it can be freely designed and placed on the one hand and freely accessible on the other, whereby during the filling of the catalyst space of the catalyst manifold can be refilled by an operator readily with catalyst material. A filling device according to the invention is preferably permanently installed in the fixed bed reactor and is preferably not removed again after completion of the filling process, so that the design freedom is not limited by an expansion possibility to be provided.

After completion of the filling, the top of the catalyst bed is located at the lower tube ends of the filling tubes. Since the filling device preferably remains in the fixed bed reactor, the filling tubes and the catalyst distributor can remain filled with catalyst material, so that further catalyst material automatically trickles into the catalyst space during reactor operation in case of settling of the catalyst bed until the desired height of the catalyst bed is reached again, d. H. until the top of the catalyst bed has again reached the lower tube ends of the filling tubes. Thus, the maintenance of the optimum height of the catalyst bed is always guaranteed.

The capacity of the filling device and the dimensions and distances of the relevant parts of the apparatus are preferably dimensioned so that even when settling the top of the catalyst bed is always safely above a predetermined minimum catalyst height. To limit bypass flows in the upper region of the catalyst bed and above, it makes sense to fill the area above the minimum height of the catalyst bed with an additional inert bed. The inert bed can also be supplied via the filling device, if the amount of catalyst is sufficient, or through the gap between the heat carrier collector and the reactor jacket or through an opening in the heat carrier collector. For this purpose, for example, the gas-impermeable upper end of the central tube can be removed for a short time. Likewise, openings can be created in the impermeable region in the outer wall of the reaction space for this filling process. The dead space below the heat transfer medium collector can be effectively minimized by an upper inert bed thus produced.

Preferably, the reactor shell forms the catalyst support. An additional component for horizontal support of the catalyst bed is thereby avoided.

In another, likewise preferred embodiment of the invention, the bundle of heat exchange tubes and the catalyst bed are annularly formed with a tube and catalyst-free inner cavity, wherein the catalyst bed is supported by a radially outer and a radially inner catalyst holder and between the reactor shell and radially outer catalyst holder outer cavity is arranged. The inner and the outer cavity can be used for the supply of the feed gas or for the discharge of the product gas. In addition, reactions are avoided in the edge region of the fixed bed reactor, in which the reaction conditions can be subject to interference.

Advantageously, the catalyst support is the surface of a bed in the lower reactor hood. The construction of the fixed bed reactor is thereby simplified, since no separate component must be provided as a catalyst support.

Preferably, the catalyst manifold is disposed horizontally outside the bundle of heat exchange tubes. In this way, the space vertically above the bundle of heat exchange tubes for other components, such as e.g. a heat transfer manifold or collector used.

In a favorable development of the invention, only one catalyst distributor is formed and extends annularly along the inside of the reactor jacket over the entire circumference. With these measures, the catalyst manifold is arranged both space-saving and freely accessible in the fixed bed reactor.

In this case, the catalyst distributor is preferably formed in cross section in the form of a trough, open into the bottom of the filling tubes and the walls are inclined to the mouth of the filling tubes. In another embodiment, the walls can also run vertically. In this way, the catalyst manifold can be structurally simple and it is ensured that all the catalyst material present in the trough reaches the junctions of the filling tubes.

In a preferred embodiment of the invention, a heat carrier distributor or collector (depending on the direction of flow of the heat carrier) is arranged above the cross-sectional area of the bundle of heat exchange tubes and the catalyst distributor over the dead space between the heat carrier distributor or collector and the reactor jacket. With such an arrangement of heat carrier distributor or collector and catalyst distributor, the space above the heat exchange tubes is used to save space.

In this case, the upper tube ends of the heat exchange tubes are advantageously tightly welded in respective through holes of an upper tube plate and the tubesheet is the bottom of the heat carrier distributor or collector and open the heat exchange tubes in this heat carrier distributor or collector. In this way, a fixed bed reactor according to the invention can be manufactured even more cost-effectively, since a separate component for the bottom of the heat transfer medium distributor or collector is omitted.

In this case, the filling tubes each particularly preferably have a first section which extends vertically downwards from the catalyst distributor between the heat carrier distributor or collector and the reactor jacket into the dead space, and a second section which extends radially inwards from the first section. In this embodiment, the first sections of the filling tubes run in a space-saving manner concentrated between heat carrier distributor or collector, d. H. upper tube plate, and reactor jacket and then distribute themselves in the form of an ostrich with its second sections above the catalyst space.

The filling tubes can also be passed in the case of multipart heat transfer manifolds and / or collectors between two heat carrier distributors or collectors. It is also possible to pass filling tubes through heat transfer manifold or collector.

In an advantageous embodiment of the invention, the lower tube ends of the filling tubes are distributed so that they each fill equal volume fractions of the catalyst bed. As a result, a largely uniform density of the catalyst bed over its entire cross-section is achieved.

The filling tubes preferably have an oval cross-section. Such shaped filling tubes can easily run with the smaller cross-sectional dimension in narrow spaces between heat exchange tubes and still have due to the larger in the vertical direction to larger cross-sectional dimension a sufficiently large tube cross-section in order to achieve a sufficient trickling speed and / or to avoid clogging of the tubes ,

It is advantageous if, in the operating state of the fixed bed reactor, the catalyst space, the filling tubes and each catalyst distributor are filled with catalyst material. As a result, even during a reactor operation in case of possible settling of the catalyst bed catalyst material automatically trickle into the catalyst space and refill the catalyst bed again. The reactor operation is thus consistent with the optimum height of the catalyst bed.

Preferably, each filling tube has a throttle. In this way, the internal dimensions of the filling tubes can be chosen so that their clogging with catalyst material is excluded, and can be selected by means of the throttle, the access cross-section for each filling tube so as to give the desired trickling speed.

In this case, the size of the throttle openings is particularly preferably adjustable. As a result, the size of the throttle openings and thus the trickling speed can be readily adapted to changed conditions even during a running filling operation.

The invention will be explained below with reference to embodiments and figures. Showing:

1 a longitudinal section through an axially traversed isothermal fixed bed reactor with a catalyst filler according to the invention;

2 a longitudinal section through a radially flowed through isothermal fixed bed reactor with a catalyst filler according to the invention, and

3a on an enlarged scale, a cross section through a catalyst manifold with a filling pipe connected thereto and

3b a cross section along line IIIb-IIIb in 3a ,

The exemplary embodiments of fixed bed reactors according to the invention shown in the figures 1 - Shortened in the following referred to as "reactor 1" - have a reactor jacket 3 , an upper and lower reactor hood 4 . 5 , a bundle of vertical heat exchange tubes 9 , a catalyst room 49 and a filling device 51 for filling the catalyst space 49 with catalyst material on.

The reactors 1 are aligned vertically, ie the respective reactor axis 6 runs vertically. The reactor jacket 3 each is a circular cylinder, which is the bundle of heat exchange tubes 9 and the catalyst room 49 encloses. At its two ends is the reactor jacket 3 from the reactor hoods 4 . 5 closed, which are tightly connected with him.

At the in 1 illustrated embodiment, the catalyst space extends 49 or the catalyst bed filled in it 8th in the horizontal direction over the entire cross-section within the reactor shell 3 ie the horizontal cross-section through the catalyst bed 8th is a circular area whose edge is the inner wall of the reactor shell 3 forms.

Accordingly, the heat exchange tubes 9 in the catalyst bed 8th also distributed on a circular area, ie a horizontal cross section through the bundle of heat exchange tubes 9 essentially also occupies a circular area. Here are the radially innermost heat exchange tubes 9 approximately circular around the reactor axis 6 arranged and the radially outermost heat exchange tubes 9 approximately circular with a predetermined distance to the inner wall of the reactor shell 3 arranged.

The terms "substantially" and "approximately" are intended to indicate that the radially innermost and outermost heat exchange tubes 9 Due to the design, they may not lie exactly on a circular line, but are displaced radially by a maximum of two pipe pitches.

The catalyst bed 8th lies on the outsides of the heat exchange tubes 9 and is in the operating state of the reactor 1 of reaction gas 15 flows through.

In this embodiment, reaction gas flow 15 and heat transfer medium 25 in the catalyst bed 8th in countercurrent, the reaction gas 15 from top to bottom and the heat transfer medium 25 from the bottom up.

That in the reactor 1 entering gas is called feed gas 16 denotes the catalyst bed 8th flowing, reacting gas as the reaction gas 15 and that from the reactor 1 escaping gas as product gas 19 ,

The feed gas 16 is in this embodiment by a gas inlet line 17 in the upper reactor hood 4 initiated and the product gas 19 through a gas outlet pipe 20 from the lower reactor hood 5 derived.

The lower ends of the heat exchange tubes 9 are in through holes of a lower tube plate 24 tightly welded and discharge into a heat transfer manifold 28 whose bottom is the bottom tube sheet 24 forms.

The upper ends of the heat exchange tubes 9 are in through holes of an upper tube plate 23 tightly welded and discharge into a heat transfer collector 30 whose bottom is the upper tube sheet 23 forms.

The lower reactor hood 5 spans the heat carrier distributor 28 and the upper reactor hood 4 the heat carrier collector 30 ,

In one embodiment, not shown, the heat transfer manifold 28 and / or the heat transfer collector 30 also be executed in several parts.

In the illustrated embodiment are heat transfer manifolds 28 and heat transfer collectors 30 ring-shaped, wherein the reactor axis 6 each passes through the ring center. The inner diameter of the rings is chosen so that the radially innermost heat exchange tubes 9 straight line between heat transfer manifold 28 and heat transfer collectors 30 can run. The outer diameter of the rings is smaller than the outer diameter of the bundle of heat exchange tubes 9 , so that radially further outward heat exchange tubes 9 have cranked pipe ends to enter the heat transfer manifold 28 or collector 30 to be able to lead. Halfway between the heat transfer manifold 28 and heat transfer collectors 30 go through the heat exchange tubes 9 a horizontal grid 37 that the heat exchange tubes 9 stabilized in the horizontal direction.

In an embodiment not shown here, a plurality of holding grids 37 be arranged in the vertical direction.

The heat carrier distributor 28 is at least one heat carrier supply line 26 connected. In the illustrated embodiment, there are two heat carrier supply lines 26 coming from outside the reactor 1 vertically through the lower reactor hood 5 run.

The heat carrier collector 30 is at least one heat transfer line 32 connected. In the illustrated embodiment, there are two heat carrier drain lines 32 passing horizontally through the reactor jacket 3 run outwards.

The catalyst bed 8th extends in the vertical direction exclusively over the area in which all heat exchange tubes 9 have straight sections, ie not into the areas in which the radially outer heat exchanger tubes 9 are cranked.

Under the catalyst bed 8th is a bed of inert material - hereinafter also referred to as lower inert bed 14a designated - which is the lower part of the reactor 1 ie the lower reactor hood 5 and the lower part of the reactor shell 3 , to the beginning of the straight heat exchange tube sections in the bent heat exchange tubes 9 and thus until the beginning of the catalyst bed 8th fills. The top of the lower inert bed 14a therefore forms a catalyst support for vertical support of the catalyst bed 8th and thus to their limitation down.

The upper limit of the catalyst space 49 and thus the desired height of the catalyst bed 8th , ie the top, is located at a predetermined distance to the bottom of the upper tube sheet 23 or the heat transfer medium collector 30 , The space formed by this distance becomes dead space 50 designated.

The filling device 51 is above the catalyst space 49 arranged and has a catalyst distributor 52 and a variety of filling tubes 48 / 53 on.

The catalyst distributor 52 is annular and in the reactor 1 above the heat carrier collector 30 arranged. The cross section of the catalyst distributor 52 is trough-shaped with a bottom 54 and walls 55 going to the ground 54 tapering towards each other.

The filling pipes 48 / 53 are with their upper ends tight in through holes 56 (S. 3a ) in the ground 54 the catalyst distributor 52 fastened and open in these, see detailed representation in 3a , They run from the catalyst distributor 52 out initially bundle-shaped outward towards the reactor jacket 3 and then between the outer edge of the heat transfer medium collector 30 and the inner wall of the reactor shell 3 down into the dead space 50 into it. There they branch off and run in different directions and with different lengths in the spaces between the heat exchange tubes 9 , Wherein the entirety of the lower tube ends of the filling tubes 48 / 53 substantially uniform over the entire cross section of the catalyst space 49 is distributed. The filling pipes 48 / 53 have a minimum inclination over their entire length, which is a perfect flow or trickling of the catalyst material in the filling tubes 48 / 53 guaranteed.

In one embodiment, not shown, filling tubes 48 / 53 in multi-part heat transfer manifolds 28 and / or collectors 30 between two heat transfer manifolds 28 or collectors 30 be passed. It is also possible to fill pipes 48 by heat transfer manifold 28 or collector 30 pass therethrough.

The inner dimensions of the filling tubes 48 / 53 are designed so that only a given amount of catalyst material per unit time each filling tube 48 / 53 can go through, ie that results in a given trickle speed.

The filling device 51 remains permanently in the reactor 1 , Therefore, the heat transfer manifolds 28 and / or collectors 30 be designed freer, for example, with regard to easier accessibility to the heat exchange tubes 9 and regardless of an expansion option.

The upper reactor hood 4 has a catalyst filler neck 57 through, through it by means of a suitable device, the catalyst manifold 52 can be filled with catalyst material.

The lower reactor hood 5 has a catalyst discharge nozzle 58 through, through which the lower inert bed 14a and the catalyst bed 8th from the reactor 1 can be removed again.

Further, in the upper reactor hood 4 another manhole 59 trained, through which a fitter for maintenance and repair work in the upper area, ie above the heat transfer medium collector 30 , can get on. This manhole 59 can also be used to supply the catalyst.

In addition, the heat carrier supply line 26 and / or the heat carrier drain line 32 be designed so that through them access into the reactor interior is possible.

Unless otherwise described below, the embodiment corresponds to 2 the embodiment according to 1 ,

At the in 2 illustrated embodiment of a reactor according to the invention 1 is the catalyst space 49 or the catalyst bed 8th annular with a catalyst-free inner cavity 11 and a catalyst-free outer cavity 12 along the inner wall of the reactor shell 3 educated. On its radially outer side is the catalyst bed 8th from a cylindrical gas-permeable outer wall 10 enclosed. Between this outer wall 10 and the inner wall of the reactor shell 3 is the outer cavity 12 educated. At its radially inner side is the catalyst bed 8th on a gas-permeable central tube 13 on or is limited by this, the axis of which on the reactor axis 6 lies.

According to the annular formation of the catalyst bed 8th is also the bundle of heat exchange tubes 9 ring-shaped. Here are the radially innermost heat exchange tubes 9 at a predetermined distance from the radially inner boundary of the catalyst bed 8th and the radially outermost heat exchange tubes 9 at a predetermined distance to the radially outer boundary of the catalyst bed 8th arranged.

In this embodiment, the gas flows from bottom to top, using it as feed gas 16 in the lower end of the gas inlet line 17 is initiated and in the catalyst bed 8th through the gas-permeable wall of the central tube 13 in the catalyst bed 8th flows in, this substantially radially as a reaction gas 15 flows through and then in the outer cavity 12 vertically upwards to a gas outlet pipe 20 flows and out of this as product gas 19 exit.

As the heat carrier 25 also flows from bottom to top, in this embodiment, a direct current of heat transfer 25 and gas available.

All heat exchange tubes 9 run in this embodiment in a straight line over its entire length. As in the embodiment according to 1 are the lower ends of the heat exchange tubes 9 in through holes of a lower tube plate 24 tightly fastened and open into a heat transfer manifold 28 whose bottom is the bottom tube sheet 24 forms. Furthermore, the heat carrier distributor 28 a distributor hood 27 on top of the lower tubesheet 24 spanned and tightly connected to this.

The upper ends of the heat exchange tubes 9 are in through holes of an upper tube plate 23 tightly fastened and open into a heat transfer collector 30 whose bottom is the upper tube sheet 23 forms and further a dome-shaped in this embodiment collector hood 31 which has the upper tube sheet 23 spanned and tightly connected to this.

In the collector's hood 31 is a collector manhole 33 designed to provide an installer for maintenance and repair access to the heat exchange tubes 9 to enable.

The heat carrier distributor 28 and the heat carrier collector 30 are annular, each having a central passage opening, which is the central tube 13 in the case of the heat transfer manifold 28 passes through and into the central tube 13 in the case of the heat transfer medium collector 30 extends for a given distance.

The radially outer edge of heat transfer manifold 28 and heat transfer collectors 30 lies between the radially outer heat exchanger tubes 9 and the radially outer boundary of the catalyst bed 8th , so that between the radially outer edge of the heat transfer manifold 28 (and also of the heat carrier collector 30 ) and the inner wall of the reactor shell 3 an annular gap is formed whose radial extent is greater than that of the outer cavity 12 ,

The heat carrier distributor 28 is at least one heat carrier supply line 26 connected. In 2 are two heat carrier supply lines 26 shown running vertically and through the lower reactor hood 5 extend to the outside.

The heat carrier collector 30 is at least one heat transfer line 32 connected. In 2 are two heat carrier drain lines 32 shown vertically through the upper reactor hood 4 through to the outside and in turn to an outer, annular heat transfer medium collector 60 are connected. The outer heat carrier collector 60 is in turn to a horizontal heat carrier drain line 61 connected.

The vertical heat carrier drain lines 32 between the one in the upper reactor hood 4 located heat carrier collector 30 and the outer heat carrier collector 60 point inside the upper reactor hood 4 one compensator each 35 to compensate for different thermal expansions.

Halfway between the lower and upper tubesheet 24 and 23 or between heat transfer manifold 28 and heat transfer collectors 30 is for horizontal stabilization of the heat exchange tubes 9 a horizontal grid 37 arranged, which is the heat exchange tubes 9 run through.

The central tube 13 extends down through the lower reactor hood 5 through and beyond this outwards and forms a gas inlet line 17 for the feed gas 16 , From the lower end, ie from the inlet opening for the feed gas 16 , until the lower beginning of the catalyst bed 8th is the wall of the central tube 13 gas impermeable trained.

At its upper end, the central tube extends 13 into the central opening of the annular heat transfer medium collector 30 , In its upper end area is the central tube 13 also with a gas-impermeable wall 21 formed, extending from the top of the central tube 13 up to a predetermined distance in the catalyst bed 8th extends into it. The upper end of the central tube 13 is gas-tight.

The lower part of the reactor 1 - ie the lower reactor hood 5 and the lower part of the reactor shell 3 to the lower end of the catalyst bed 8th - is also here with a lower inert bed 14a filled. The top of this lower inert bed 14a thus forms the lower boundary and vertical support for the catalyst bed 8th ,

At the in 2 illustrated embodiment, the catalyst manifold extends 52 the filling device 51 annular along the inside of the reactor shell 3 over its entire circumference. He is above the gap or annular gap between the outside of the heat transfer medium collector 30 and the inner wall of the reactor shell 3 arranged so that the filling tubes 53 from the ground 54 the catalyst distributor 52 from to below the upper tube bottom 23 or the heat transfer medium collector 30 extend vertically and then as in the embodiment according to 1 in the form of an ostrich in the bundle of heat exchange tubes 9 branch into it.

In 2 is the state after complete filling of the catalyst space 49 represented with catalyst material, ie the top of the catalyst bed 8th lies at the lower tube ends of the filling tubes 53 at. The filling pipes 53 and the catalyst manifold 52 are still filled with catalyst material, so that when setting the catalyst bed 8th Even during reactor operation, catalyst material automatically into the catalyst space 49 is refilled. In this embodiment, there is still an upper inert bed 14b over the catalyst bed 8th ,

The upper reactor hood 4 has, as in the embodiment according to 1 , a catalyst filler neck 57 and a manhole 59 on.

Likewise, the lower reactor hood 5 as in the embodiment according to 1 , a catalyst discharge nozzle 58 on.

The in 2 represented reactor 1 also has a fluidizing device 62 for emptying the reactor 1 on. They include distribution lines 63 for a fluidizing gas between the catalyst bed 8th and the heat transfer manifold 28 in the lower inert bed 14a run. The distribution lines 63 have a loop 64 on top of that bunch of heat exchange tubes 9 runs around and to a gas supply line 65 connected horizontally through the reactor jacket 3 extends outwards and outside the reactor shell 3 a compressor 66 having. The gas can be supplied in a dehumidified state at elevated pressure and pulsating continuously or with pressure surges. Furthermore, the distribution lines 63 still radial branches 67 on that with the loop 64 fluidly connected and within the lower inert bed 14a into the bundle of heat exchange tubes 9 extend into and out of which the fluidizing gas exits. Optionally, there are further, preferably separately operable, lower branch lines 68 , which are below the bundle of heat exchange tubes 9 are arranged.

In 3a is on an enlarged scale the connection of the upper pipe end of a filling tube 53 to the ground 54 the catalyst distributor 52 shown. The upper tube end of the filling tube 53 has a radially expanded shoulder portion 69 on that with the ground 54 the catalyst distributor 52 is tightly connected. The floor 54 indicates a slope to the mouth of the filling tube 53 so that catalyst material from the side areas of the catalyst manifold 52 slides towards the junction. In the shoulder section 69 at the upper tube end of the filling tube 53 is a throttle 70 with a throttle opening 71 arranged, by means of the per unit time in the filling tube 53 entering amount of catalyst material and thus the rate of trickling out of the filling tube 53 exiting catalyst material is set.

The filling tube 53 has an oval cross section ( 3b ). The smaller cross-sectional dimension 72 is due to the size of the gap between adjacent heat exchange tubes 9 through which the filling tube passes 53 runs, determined. The size of the larger cross-sectional dimension 73 is set so that the free passage cross section 74 of the filling tube 53 is sufficiently large compared to the dimensions of the catalyst particles, to jamming of catalyst particles and thus clogging of the filling tubes 53 to avoid.

LIST OF REFERENCE NUMBERS

1

 reactor

2

 pressure shroud

3

 reactor shell

4

 Upper reactor hood

5

 Lower reactor hood

6

 Central axis / reactor axis

8th

 catalyst bed

9

 Heat exchange tubes

10

 Outer wall of the reaction space

11

 Inner cavity

12

 Outer cavity

13

 Central tube / inner wall of the reaction space

14a

 Lower inert bed

14b

 Upper inert bed

15

 reaction gas

16

 feed gas

17

 Gas inlet pipe

19

 product gas

20

 Gas discharge line

21

Impermeable area in the central tube

22

 Impermeable area in the outer wall of the reaction space

23

 Upper tube sheet

24

 Lower tube sheet

25

 heat transfer

26

 Heat transfer supply line

27

 distribution hood

28

 Heat transfer manifold

30

 Heat carrier collector

31

 collectors hood

32

 Heat carrier drain pipe

33

 Collectors manhole

35

 compensator

37

 holding grid

48

Fill pipes through the heat carrier collector

49

catalyst chamber

50

dead space

51

 filling

52

catalyst distribution

53

filling tubes

54

Bottom of the catalyst distributor

55

Walls of the catalyst distributor

56

Through holes

57

Katalysatorfüllstutzen

58

Catalyst drain nozzle

59

manhole

60

Annular heat carrier collector

61

Horizontal heat carrier drain line

62

fluidisation

63

distribution lines

64

loop

65

Gas supply line

66

compressor

67

branch lines

68

Lower branches

69

 shoulder portion

70

throttle

71

 throttle opening

72

 Smaller cross-sectional dimension

73

Larger cross-sectional dimension

74

Passage section

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

• US 4321234 [0004]
• US 7353847 B2 [0005]
• US 6467513 B1 [0006, 0007]
• US 4,277,205 [0009]
• DE 19634455 A1 [0011]
• EP 2029463 A1 [0012]
• DE 2849664 A1 [0013]
• US 4402643 [0014]
• EP 0963785 A1 [0015]

Claims (16)

Fixed bed reactor for carrying out catalytic gas phase reactions, comprising a bundle of vertical heat exchange tubes ( 9 ), the lower and upper pipe ends to each at least one heat carrier distributor ( 28 ) or collectors ( 30 ) are connected; a catalyst space ( 49 ) for receiving a catalyst bed ( 8th ), which on the outer sides of the heat exchange tubes ( 9 ) and in the operating state of the fixed bed reactor ( 1 ) of reaction gas ( 15 ) is flowed through, wherein the catalyst space ( 49 ) is bounded horizontally by a catalyst support, which for horizontal support of the catalyst bed ( 8th ) and vertically downwardly from a catalyst support ( 14 ) is limited to the vertical support of the catalyst bed ( 8th ) is formed, and extends to a predetermined height, so that between the upper limit of the catalyst space ( 49 ) and the upper tube ends of the heat exchange tubes ( 9 ) a dead space ( 50 ) is trained; a reactor jacket ( 3 ) containing the bundle of heat exchange tubes ( 9 ) and the catalyst space ( 49 ) encloses; an upper and lower reactor hood ( 4 . 5 ), the upper or lower tube ends of the heat exchange tubes ( 9 ) and the respective at least one heat carrier distributor ( 28 ) or collectors ( 30 ) and supply and discharge lines ( 17 . 20 . 26 . 32 ) for feed or product gas ( 16 . 19 ) and / or heat transfer medium ( 25 ) and in each case with the reactor jacket ( 3 ) are tightly connected; and with a filling device ( 51 ) for filling the catalyst space ( 49 ) with catalyst material above the catalyst space ( 49 ) and has at least one catalyst distributor ( 52 ) outside the bundle of heat exchange tubes ( 9 ) is arranged, and a plurality of filling tubes ( 53 ), with their upper tube ends in each case in the at least one catalyst distributor ( 52 ) flow into the dead space ( 50 ) extend into it and open with their lower tube ends in this, wherein in the dead space ( 50 ) the course of all filling tubes ( 53 ) is coordinated so that the entirety of its lower tube ends over the entire cross section of the catalyst space ( 49 ) is distributed. Fixed bed reactor according to claim 1, characterized in that the reactor jacket ( 3 ) forms the catalyst holder. Fixed bed reactor according to claim 1, characterized in that the bundle of heat exchange tubes ( 9 ) and the catalyst bed ( 8th ) annularly with a tube and catalyst-free inner cavity ( 11 ) are formed, wherein the catalyst bed ( 8th ) of a radially outer and a radially inner catalyst holder ( 10 . 13 ) and between reactor shell ( 3 ) and radially outer catalyst support ( 10 ) an outer cavity ( 12 ) is arranged. Fixed bed reactor according to one of claims 1 to 3, characterized in that the catalyst support the surface of a bed ( 14a ) in the lower reactor hood ( 5 ). Fixed bed reactor according to one of claims 1 to 4, characterized in that the catalyst distributor ( 52 ) horizontally outside the bundle of heat exchange tubes ( 9 ) is arranged. Fixed bed reactor according to one of claims 1 to 5, characterized in that only one catalyst distributor ( 52 ) is formed and this annularly along the inside of the reactor shell ( 3 ) extends over the entire circumference. Fixed bed reactor according to claim 6, characterized in that the catalyst distributor ( 52 ) is formed in cross-section in the form of a trough, in the bottom ( 54 ) the filling tubes ( 53 ) and whose walls ( 55 ) to the mouth of the filling tubes ( 53 ) inclined. Fixed bed reactor according to one of claims 1 to 7, characterized in that a heat carrier distributor ( 28 ) or collector ( 30 ) over the cross-sectional area of the bundle of heat exchange tubes ( 9 ) and the catalyst distributor ( 52 ) above the dead space ( 50 ) between the heat carrier distributor ( 28 ) or collector ( 30 ) and the reactor jacket ( 3 ) is arranged. Fixed bed reactor according to claim 8, characterized in that the upper tube ends of the heat exchange tubes ( 9 ) in respective through holes of an upper tube plate ( 23 ) are tightly welded and the tubesheet ( 23 ) the bottom of the heat carrier distributor ( 28 ) or collector ( 30 ) and the heat exchange tubes ( 9 ) in this heat transfer manifold ( 28 ) or collector ( 30 ). Fixed bed reactor according to claim 8 or 9, characterized in that the filling tubes ( 53 ) each have a first portion extending from the catalyst manifold ( 52 ) from between heat carrier distributor ( 28 ) or collector ( 30 ) and reactor jacket ( 3 ) vertically down to the dead space ( 50 ) and a second portion extending radially inwardly from the first portion. Fixed bed reactor according to claim 8 or 9, characterized in that a part or all filling tubes ( 48 ) by the heat carrier distributor ( 28 ) or collector ( 30 ) are passed. Fixed bed reactor according to one of claims 1 to 11, characterized in that the lower tube ends of the filling tubes ( 53 ) are distributed so that they each equal volume fractions of the catalyst bed ( 8th ) to fill. Fixed bed reactor according to one of claims 1 to 12, characterized in that the filling tubes ( 53 ) have an oval cross-section. Fixed bed reactor according to one of claims 1 to 13, characterized in that in the operating state of the fixed bed reactor ( 1 ) the catalyst space ( 49 ), the filling tubes ( 53 ) and each catalyst distributor ( 52 ) are filled with catalyst material. Fixed bed reactor according to one of claims 1 to 14, characterized by a throttle ( 70 ) for each filling tube ( 53 ). Fixed bed reactor according to claim 15, characterized in that the size of the throttle openings ( 71 ) is adjustable.

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