TURBULENCE INDUCER IN CHEMICAL REACTOR

Abstract: The invention concerns improvements in catalytic converters for optimising the ratio of pressure drop to mass transfer of gases flowing through the catalytic converter. For this purpose, the latter is provided with channels (1) formed with turbulence generators (3, 4) extending transversely in the path of flow of the gases. In order to obtain this object, the structure of the catalytic converter should satisfy certain distinct conditions. These conditions refer to the distance from the catalytic converter inlet (1) to the center of the turbulence generator (3) positioned closest to said inlet, the angle defining the inclination of the trailing edge face (5) of the turbulent generators (3, 4) relatively to a vertical plane through the bottom (8) of the catalytic converter channel (2), the ratio of the height of the upper face (6) above the bottom (8) to the hydraulic diameter of the channel (2), the ratio of the distance between the centers of the first (3) and the second turbulence generators (4), as seen from the inlet (1), to said height, and the ratio of the length of the upper face (6) of each turbulence generator (3, 4) to the height of said face above the catalytic converter bottom (8).

Description: TURBULENCE INDUCER IN CHEMICAL REACTOR The invention relates to improvements in catalytic converters for optimising the ratio between pressure drop and mass transfer of gases. Usually, a catalytic converter has a substrate constructed from a considerable number of neighbouring small channels, through which flows a gas or a gas mixture to be converted. Various materials may be used to construct, catalytic converters, such as ceramic materials, or metal, e.g. stainless steel or aluminium. The cross-section of the channels of ceramic catalytic converter substrates usually is rectangular or polygonal, i.e. hexagonal. This type of catalytic converters are manufactured by extrusion, a method that produces channels having the same cross-section along their entire length and channel walls that are smooth and even. In the manufacture of catalytic converter substrates from metal, one corrugated strip and one flat strip usually are wound together upon themselves aoout an axis. The resulting channel cross-sectional shape is triangular or trapezoidal. The metal catalytic converters that are available on the market are formed with channels having an equal cross-sectional size along their entire length and, like the ceramic catalytic converter substrates, their channel walls are smooth and even. The most essential feature is the mass transfer that takes places between the gas or the gas mixture flowing through the channels and the catalytic converter channel walls. The coefficient of mass transfer, which is a measure of the mass transfer rate, must be high f high efficiency of catalytic conversion is to be achieved. In catalytic converters of the kind mentioned above, which are used m internal combustion engines or in industry and the channels of which have a comparatively small cross-sectional shape, the gas, at the gas velocities common m these contexts, flows in comparatively regular layers in the direction of the channels. Thus, the flow is mainly laminar. Only along a shorter length adjacent the channel inlets does some cross-wise flow take place in the direction towards the channel walls. To categorize the gas flow the so called Reynolds number is used, the value of which in these applications is between 100 and 600. As long as the Reynolds number remains lower than approximately 2000, the flow remains laminar. It is well known withm the technical field concerned, that in laminar gas flows a boundary layer is formed closest to the channel walls, in which boundary layer the gas velocity is substantially zero. This boundary layer strongly reduces the coefficient of mass transfer, above all in the case of so called fully developed flow. In order to increase the coefficient of mass transfer, the gas must be made to flow towards the channel surface, which reduces the boundary layer and increases the flow transfer from one layer to another. This may be effected by turbulent flows. In smooth and even channels the laminar flow turns turbulent when the Reynolds number reaches values above approximately 2000. If one wishes to reach a Reynolds number of this magnitude m the channels of the type of catalytic converters concerned herein, considerably higher gas velocities than is conventional in these contexts are required. For the low Reynolds number values involved in catalytic converters of the kind referred to above t is therefore necessary to create turbulence by artificial means, for instance by arranging special turbulence generators inside the channels. A large number of turbulence generators are already known. From SE-B-461 018 is known a catalytic converter having channels w th turbulence generators therein in the form of transverse corrugations. From GB-A-2001547 is known a catalytic converter having channels in which turbulence generators in the form of transverse metal flaps punched from the structural material are provided. Also combinations of these two types of turbulence generators exist. A feature common to turbulence generators of this kind is their ability to significantly increase the mass transfer. However, also the pressure drop increases dramatically. In fact, the pressure drop increase has proved to exceed the increase of mass transfer. The pressure drop as such depends on the configuration, dimensions and geometry of the turbulence generators. However, it is well known that said types of turbulence generators produce a pressure drop that is too high, which has prevented them from being used commerci-ally to any significant extent. The invention is based on the realisation that the turbulence generators should be so placed and so configured in the catalytic converter channels that an optimal ratio of pressure drop to mass transfer is obtained. In the application concerned here, reference is made to the concept hydraulic diameter, which is an expression denoting the ratio of the through-flow channel cross-section area to the channel perimeter. At the inlets of the catalytic converter channels the coefficient of mass transfer is high because the boundary layer is very thin. The thickness of the boundary layer gradually increases in the direction of the main flow and the coefficient of mass transfer, i.e. the rate of the transfer of mass towards the channel surface is reduced. In order to increase the mass transfer, and consequently the efficiency of the catalytic conversion, turbulence generators should not be positioned in the channel walls too close to the inlets, since the mass transfer is already high in this area. Overall, the provision of turbulence generators in this area therefore would only cause an increase of the pressure drop, which is not desirable. The invention is characterised in that in order to meet the above-mentioned objects the structure of the catalytic converter should satisfy certain conditions as defined in the appended claims. The invention will be explained more detail in the following with reference to the accompanying drawing, wherein, Fig. 1 is a perspective view showing a channel of a catalytic converter, formed with turoulence generators in accordance with the mvention, Fig. 2 illustrates the same channel schematically in a lateral view and Fig. 3 is a cross-sectional view through the channel in the area of a turbulence generator. In the drawing are shown the inlet 1 and a part of a channel 2 in a catalytic converter in accordance with the invention. The drawing shows only a first turbulence generator 3 positioned closest to the inlet 1 and a second turbulence generator 4 . The channel 2 has a height h. The distance Xi from the mlet opening to the center of the first turbulence generator 3 is determined by the following expression: 0.01 < > 0.015 Dh ' Re • Sc wherein Dh is the hydraulic diameter of the channel Re is the Reynolds number Sc is the Schmidt's number of the gas mixture. It is apparent from this expression that Xi depends on the Reynolds number and thus on the gas velocity. The optimal position of the first turbulence generator 3 thus depends on the prevailing operating conditions. As appears particularly from Fig. 2, the turbulence generators 3,4 are given a specific geometry configura- tion. Thus, they may be formed with a sloping trailing edge face 5, a flat top face 6 and an oblique front edge face 7. In accordance with the invention the following conditions apply: the angle θ defining the inclination of the trailing edge face 5 of the turbulence generators 3,4 relatively to the bottom 8 of the catalytic converter channel 2 should be between 35 and 50 degrees and the ratio of the height e of the upper face 6 above the bottom 8 to the hydraulic diameter D of the channel 2 should be between 0.35 and 1.0. In addition, the ratio of the distance P between the centres of the first and the second turbulence generators 3 and 4 to said height dimension e should be between 20 and 50 and the ratio of the length B of the top face 6 of each turbulence generator 3, 4 to the height e of the top face above the catalytic converter bottom 8 should amount to between 1.5 and 4.0. By configuring, in accordance with the teachings of the mvention, the turbulence generators 3, 4 with a specific geometry configuration and positioning them at pre-determined distances from one another and from the inlet 1 in channels 2 having a preferably triangular and/or trapetzoidal cross-sectional shape, an increased mass transfer is achieved, and consequently also increased catalytic conversion but accompanied by only a moderate pressure-drop increase. When the gas flow approaches the turbulence generator 3 the flow velocity increases locally due to the reduced cross-sectional area, a feature which Fig. 3 is intended to illustrate. When the gas thereafter passes the turbulence generator 3 and leaves the edge formed at the junction between the top face 6 and the front edge face 7 a violent turbulent motion arises on account of such separation and the highly diverging cross-sectional area. This process very efficiently increases the mass transfer. The turbulence generator 4 is located at a calculated distance P from the first turbulence generator 3 to allow the turbulence thus created to be made use of as completely as possible and in order for a re- contactmg zone, indicated by 0 m Fig. 1, to form before the gas passes the turbulence generator 4. In this manner unnecessary excess pressure drop is prevented without a significant increase of the mass transfer in the already turbulent gas flow. In the re-contacting zone 0 the gas will again to a large extent flow adjacent the smooth surface before reaching the turbulence generator . It is important that the edges of the turbulence generators 3, 4 are sufficiently sharp to create the separation points (shifting points) . The radius r, see Fig. 2, should be such that the ratio r: Dh is between 0.04 and 0.2. By configuring the turbulent generators in accordance with the teachings of the invention they become efficient also at the high gas velocities at which a turbulent flow would form also in a smooth channel . The turbulence that forms naturally is reinforced by the converging/diverging effect and by the mechanisms of separation and re-contacting of the gas. The mass transfer increase in accordance with the invention may be utilised in the following manner. The mass transfer j usually is determined by the expression wherein hM is the coefficient of mass transfer A is the transferring surface Wis is the mass fraction of substance 1 the gas (bulk value) i s the mass fraction of substance 1 at the surface p is the density of the gas. The expression wis - wiw is a measure of the concentration of unconverted gas. If hM increases the catalytic conversion increases for a constant size of surface A. On the other hand if it is not necessary to increase j and the mass transfer instead is maintained constant, the area of the channel surface may be reduced. It then becomes possible also to reduce the amount of carrier material (stainless steel the case of metal catalytic converters and washcoat) and the very expensive noble metals in the catalytic converter, and this manner considerable economical ga s may be made. If instead, for a given front area of the catalytic converter, it is desirable to reduce the area of the channel surface such area reduction may be done by increasing the hydraulic diameter. This reduces the pressure drop, which may be used for the extra pressure drop, resulting from the generation of the turbulence. In this manner, the pressure drop increase may be limited, despite the increase of the mass transfer (hM increases) . Consequently, the higher coefficient of mass transfer compensates for the reduced channel surface area. The amount of carrier material and washcoat, and the expensive noble metals in the catalytic converter may thus again be lessened and consequently considerable economical ga s be made. Assuming we have a straight smooth channel of predetermined dimensions. With respect to the so-called fully developed flow region the pressure drop (for a given gas velocity) is inversely proportional to the hydraulic diameter. When the hydraulic diameter is increased, for instance by a factor of 2, the pressure drop falls correspondingly. In the case of fully developed flow and mass fraction fields also the mass transferring surface is however, inversely proportional to the hydraulic diameter. Thus, also the transfer is reduced. If a comparatively large channel is provided with turbulence generators in accordance with the invention the pressure drop and the mass transfer will increase. Without reducing the mass transfer the pressure drop will be increased to the values applicable to a smaller-size channel. The exact numerical value of the mass transfer depends on the geometry of turbulence generators. When the coefficient of mass transfer reaches values twice those applicable to the smaller-size channel, the same catalytic conversion may be achieved while using almost only half the amount of the material (carrier material, washcoat and noble metals) .

Claims: CLAIMS 1. Improvements in catalytic converters for optimising the ratio of pressure drop to mass transfer of gases flowing through the catalytic converter, the latter for this purpose being provided with channels (1) formed with turbulence generators (3, 4) extending transversely in the path of flow of the gases and having a trailing edge face (5), an upper face (6), and a front edge face (7) , c h a r a c t e r i z e d in that the structure of the catalytic converters, order to meet said requirements, are to satisfy the following conditions: that the distance Xi from the catalytic converter mlet (1) to the center of the turbulence generator (3) positioned closest to said let is defined by the expression: Xi 0.01 < > 0.015 D h • Re • Sc wherein D is the hydraulic diameter of the channel R e is the Reynold' s number and Sc is the Schmidt's number of the gas mixture, the angle θ defining the inclination of the trailing edge face (5) of the turbulent generators (3, 4) relatively to a vertical plane through the bottom (8) of the catalytic converter channel (2) should be between 35 and 50°, the ratio of the height e of the upper face (6) above the bottom (8) to the hydraulic diameter D n of the channel (2) should be between 0.35 and 1.0, the ratio of the distance P between the centers of the first and the second turbulence generators (3, 4) , as seen from the let (1), to said height e should be between 20 and 50, and, the ratio of the length B of the upper face (6) of each turbulence generator (3, 4) to the height e of said face above the catalytic converter bottom (8) should be between 1.5 and 4.0.

Inventors: NILSSON SVEN MELKER, NILSSON, SVEN, MELKER
Applicants: NILSSON SVEN MELKER, NILSSON, SVEN, MELKER
Application year: 1995
Main classification: B01J35
IPC codes: B01D53, B01J35, F01N3, F01N7