Title of Invention	AN IMPROVED ROTATING TRANSFER DEVICE FOR GASEOUS EFFLUENTS
Abstract	(57) Abstract: The device mainly comprises a crown (1) of vertical axis driven into rotation in a cage (2) that is so arranged that it delimits around the crown two zones of variable section (Za, Zb) respectively intended for the inflow of the polluted effluents and for the outflow of the cleaned effluents. Cleaning is preformed by passage from one zone to the other through the crown that comprises an annular catalyst bed (9) covering its inner wall and preferably an annular load (M) outside the catalytic bed, of a material exhibiting a large heat exchange surface. Means are used for generating high pressure drops preventing leaks due to crown bypassing. A burner can be added if need be in the reaction zone. This layout allows to reduce considerably the size and the weight of the device, as well as its manufacturing and maintenance cost. The device can be used for cleaning gases loaded impounds for example. PRICE: THIRTY RUPEES

Title of Invention

AN IMPROVED ROTATING TRANSFER DEVICE FOR GASEOUS EFFLUENTS

Abstract

(57) Abstract: The device mainly comprises a crown (1) of vertical axis driven into rotation in a cage (2) that is so arranged that it delimits around the crown two zones of variable section (Za, Zb) respectively intended for the inflow of the polluted effluents and for the outflow of the cleaned effluents. Cleaning is preformed by passage from one zone to the other through the crown that comprises an annular catalyst bed (9) covering its inner wall and preferably an annular load (M) outside the catalytic bed, of a material exhibiting a large heat exchange surface. Means are used for generating high pressure drops preventing leaks due to crown bypassing. A burner can be added if need be in the reaction zone. This layout allows to reduce considerably the size and the weight of the device, as well as its manufacturing and maintenance cost. The device can be used for cleaning gases loaded impounds for example. PRICE: THIRTY RUPEES

Full Text	The invention relates to a rotating catalytic cleaning device for gaseous effluents having polluting substances suited for working as a heat exchanger and as a thermal and/or catalytic effect cleaner. The invention notably applies to heat exchange systems or to systems suited for cleaning air loaded with substances such as volatile organic compounds (VOC), that can be oxidized and eliminated by thermal or catalytic incineration. THE OF THE INVENTION The claimant's patent application 94 06,282 describes a heat exchange and thermal and/or catalytic effect cleaning device for polluted gases such as Voss. It comprises a housing or cage, a crown containing a load of solid particulate materials selected because they exhibit a large heat exchange surface (silica, granite or Günter materials such as metallic honeycomb structures or others, or cryogenic nodules for negative temperatures, etc) that is placed in the depth of the cage. The crown is split up into several parts by an inner separation or, in some cases, it serves as a support for a certain number of baskets. Motive means are used for driving the crown and the cage into a rotating motion in relation to one another about a vertical axis (either the crown rotates, the cage being stationary, or the crown is stationary and the cage rotates about it). The prior device comprises a pipe for delivering effluents into the cage and I pipe for discharging effluents out of the cage. The crown comprises a first ector for communicating continually the delivery pipe with the central part of he cage where a first heat exchange occurs between the effluents and the load n the crown. By means of a second sector of the crown where a second heat exchange takes place between effluents and the load in the crown, the central >art of the cage communicates continually with the discharge pipe. This prior device can be used only as a simple heat exchanger or for a combined use as a heat exchanger and as an incinerator for polluted effluents. In [lies case, the delivery pipe receives effluents containing polluting substances, 'he first sector and the second sector communicate directly with one another by leans of the central part of the cage. A thermal reactor possibly provided with a atalytic bed selected to bring about an exothermic reaction in the presence of le polluting substances is placed in this central part in order to burn the polluting substances in the effluents channeled by the first angular sector. With this layout, the crown rotates between two stationary parts : the entrap reactor and the housing. In order to prevent leaks due to the bypassing f the central zone reactor, it is necessary to provide a double annular seal. This ; obtained by imposing tight shape and concentricity tolerances during the manufacturing stage as well as during the mounting stage. SUMMARY OF THE INVENTION The rotating catalytic cleaning device for polluted gaseous effluents according to the invention comprises a housing or cage, a crown placed in the cage, and motive means for driving the crown into a continuous rotating motion with respect to the cage about a vertical axis, at least one pipe for delivering effluents into the cage and at least one pipe for discharging effluents out of the cage, the crown comprising at least a first sector for communicating continually the delivery pipe with the central part of the cage, and at least a second sector for communicating continually the central part of the cage with the discharge circuits and a catalytic cleaning reactor for burning the polluting substances mixed with the effluents channeled by the first angular sector. The device is characterized in that it comprises in combination at least an annular catalytic bed arranged in the inner part of the crown over the total circumference thereof and a load of a material exhibiting a large heat exchange surface arranged in the crown, outside the catalytic bed. With this layout, the polluted effluents (possibly preheated in an outer exchanger), after heating up in contact with the thermal mass in the outer part of the first angular sector of the crown, are cleaned by crossing a first time the annular catalytic bed covering the inner wall of the crown. They cross the bed a second time on the other side of the central part, before they yield part of the heat acquired by means of the catalytic incineration to the thermal mass in the second angular sector of the crown prior to their discharge. This layout of the mass having a large heat exchange surface and of the catalyst in the rotating part of the device allows the weight and the volume of the crown to be decreased, which simplifies its design. It also facilitates its assembly and lowers manufacturing and maintenance costs. The crown being within the cage, two bearings are sufficient to support its shaft and to bear the stresses. To drive it into rotation, outer motive means sufficiently distant from the warmest zones can be used and installed on top of the device, which allows its headroom to be decreased. The thickness of the catalytic bed is selected sufficient for the polluted gases to be cleaned after their two successive passages through the catalytic bed, on either side of the central part. The thermal reactor preferably comprises heating means communicating with the central zone of the crown, such as a burner arranged in a fresh effluent delivery pipe opening into the central zone of the crown or a burner placed outside the crown, above its central zone, and preferably associated in this case with means for injecting a flow of temperature regulating fresh gas into an intermediate zone between the inflow and the outflow zones. With this combination of effluent cooling and heating means, the incineration temperature can be easily regulated when it varies on account of the variation in the proportion of polluting substances in the effluents. This addition of a burner is most often necessary for starting if the polluted gases delivered are not warm enough or if the VOC proportion in the gases is not sufficient for the self-containment of the exothermic reaction in the reactor. According to an embodiment, the crown is eccentric in the cage, the latter delimiting around the crown two peripheral zones of variable section, and two intermediate zones of high pressure drop so as to prevent parasitic flows from bypassing the thermal reactor, and insulating joints can be provided between the cage and the crown. According to an embodiment, the crown is split up into several angular zones by an inner separation (8), each of these zones being filled, outside the catalytic bed, with a bulk load of a material having a large heat exchange surface. The crown can also comprise a plurality of parallelepiped chambers containing the load exhibiting a large heat exchange surface. This load exhibiting a large heat exchange surface consists for example of knitted, woven or needled metallic mats, stone blocks, a honeycomb structure or it is made from turning or machining chips. The crown and the cage comprise each an upper end part and a lower end part, and preferably seal means arranged between the corresponding walls, such as blade joints or flap joints. The upper and lower seal is easy to provide because the temperature is relatively low therein. The device can also comprise means for injecting a flow of sweep gas into an intermediate zone between the inflow and the outflow zones. The continuous cleaning process according to the invention is characterized in that it comprises establishing a permanent circulation of effluents to be cleaned on one hand between delivery pipes and on the other hand discharge pipes through a rotating crown provided with an inner separation and containing at least an annular catalytic bed arranged against its inner wall and a load of a material exhibiting a large heat exchange surface Co arranged in the crown outside titer catalytic bed, so that the effluents flow through the rotating load and heat up in contact therewith in a first heat exchange zone and, after a double passage through the rotating catalytic bed and incineration, in that they heat the thermal mass in a second heat exchange zone. With the process according to the invention, the polluting substances can be incinerated at a temperature of the order of 400 to 500°C only, which simplifies the design and reduces technical constraints, as well as the manufacturing cost. .Accordingly, the present invention provides a rotating catalytic cleaning device for gaseous effluents having polluting substances, comprising a housing or cage with a central part, a crown located within the cage and motive means for driving the crown into a continuous rotating motion around a vertical axis, at least one delivery pipe for feeding effluents into cage and at least one pipe for desiring effluents out of the cage, crown comprising at least a first in flow sector for continually communicating said delivery pipe with the central part of cage, and at least a second outflow sector of the crown for continually communicating said central part of the cage with the discharge circuits and a catalytic cleaning reactor for burning the polluting substances mixed with the effluents channelled by said first inflow sector, characterized in that it comprises in combinaticm at least an p- annular rotating catalytic bed arranged in the inner part of said crown on the total O circumference thereof and a rotating load of a material exhibiting a large heat exchange surface arranged in the crown, outside said catalytic bed Other features and advantages of the improved device according to the invention will be clear from reading the description hereafter given by way of non limiting example, with reference to the accompanying drawings in which : - Figure 1 diagrammatically shows a cross-section of an embodiment of the device, in a combined use as an incinerator for polluting substances in effluents and as a heat exchanger, and - Figure 2 shows an embodiment variant of the means for regulating the temperature of the catalytic reactor. DESCRIPTION OF THE PREFERRED EMBODIMENTS The device comprises (Figure 1) a drum consisting of a crown (1) of vertical axis arranged in a metallic outer housing or cage 2 of centrically shape for example. The diameter of the cage or housing 2 is greater than that of crown 1. The latter is offset with respect to cage 2. On either side of the diametral plane containing the vertical axis 3 of the crown, and along a Emitted angular sector, cage 2 comprises a portion of a lateral wall 4 substantially tangent to the lateral wall 5 of the crown. The inner space of the cage around crown 1, on either side of wall portion 4, thus comprises two rounded zones of variable section Za and Zb. They communicate respectively with a pipe 6 intended to deliver the gaseous effluents to be cleaned and with a pipe 7 intended to discharge these effluents after cleaning. Crown 1 is provided with an inner separation consisting of evenly distributed straight radial plates 8. A first angular sector Zl delimited by one or several of these radial plates 8 channels the effluents to be cleaned and fed into the convergent zone Za towards the central zone 11 of the crown (flow Fe). A second angular sector Z2 communicates the central zone 11 of the crown with the divergent zone Zb and with discharge pipe 7 (flow Fs). The inner wall of the crown is entirely covered with an annular catalytic bed 9 that the effluents must cross to reach the reactive central zone 11. This catalytic bed 9 consists either of a particle bed, or preferably of a honeycomb catalyst, which allows, all other things being equal, to reduce its thickness and volume, and especially to decrease the pressure drop it generates. An active mass M consisting of a material having a large heat exchange surface is arranged in the remaining part of the crown outside this catalytic bed, between the separation plates 8. It can be ceramic or metal balls, turning or machining chips, a bulk or structured packing, a honeycomb structure with regular or irregular cells such as honeycombs, knitted, woven or needled metallic mats, etc. A honeycomb structure such as that described in the claimant's patent FR-2,564,037 is advantageously used. This mass exhibiting a large heat exchange surface can also consist of stones. In order to facilitate manufacturing and loading, the crown can also be so arranged that it serves as a support for a certain number of parallelepipedic baskets 10 separate from one another, as shown in Figure 1. In the diametral plane containing the axis 3 of crown 1, the narrowness of the space remaining between the crown and cage 2, on account of its eccentricity and of wall projection 4, generates a pressure drop sufficient to prevent direct peripheral communications between the two upstream and downstream spaces Za and Zb other than through the central zone 11. Joints or flap joints 12 can be possibly placed on the periphery of the crown where the temperature is relatively low in order to complete the seal. The crown and the cage are closed at their lower and upper parts by even plates 13. Several blade joints (not shown) simultaneously resting between the corresponding plates of the crown and of the cage prevent parasitic bypassing flows between zones Za and Zb. Motive means (not shown) arranged above the cage for example are coupled with the shaft 3 of the crown for driving it into rotation with respect to cage 2. The intermediate angular sector delimited by the wall portion 4 of the cage preferably comprises a pipe 14 for injecting fresh air intended to blow off the foul effluents through the thermal mass and the catalyst in the few angular sectors of the crown passing before it, prior to each inversion of the direction of flow. After crossing the drained sectors, the sweep air mass reaches the central zone 11 where it is carried along with the main flow towards zone Zb through crown 1. In the angular sector opposite pipe 14, the cage comprises another pipe 15 (Figure 1) for injecting fresh air intended to regulate possibly the temperature of the catalytic reaction if it rises too much. The reaction that takes place in the central zone is exothermic and it is adjusted so as to release enough energy to compensate substantially for the calorific dissipation. A proportion of 0.4 g of VOC per m; of effluents is enough for an autothermal running. A burner (B) supplied with natural gas or LPG is arranged above central zone 11 for example, its flame entering directly the central zone. It is used to heat the incoming flows at the starting point if necessary, so as to reach an autothermal working point, or possibly to provide makeup heat if the polluting compounds VOC content is insufficient to obtain an autothermal running. According to the embodiment of Figure 1, the temperature in the catalytic reactor is controlled separately by means of a burner B above the crown and of a radial pipe 15 delivering fresh effluents. According to the embodiment of Figure 2, burner B can be placed in a pipe 16 opening into central zone 11 instead of being placed directly above this zone. Pipe 16 can act as a bypass line connected to the pipe 6 delivering the effluents to be treated. The flow diverted through this pipe 16 is controlled by a valve VI. Burner B is supplied with fuel by means of a control valve V2. By varying the flow of effluents diverted through pipe 16 and its temperature by means of burner B, the exothermic reaction can be controlled in the reactor. If the polluting substances concentration exceeds the autothermal limit, cold effluents are injected. On the other hand, the burner is fed if this concentration remains below this limit and during the installation starting period. After their double passage through the catalytic bed, on either side of central zone 11, the polluting compounds (VOC) are converted by the reaction into various combustion products : CO2, H2O, N2 mainly, SOx and NO; as traces. The high temperature gases coming from the reactive zone flow through the part of the load M located in the angular zone Z2 of the crown and they yield a good part of their calories thereto. The rotation of crown 1 with respect to cage 2 progressively brings the heated elements towards the angular zone Zl where they can yield in turn part of the calorific energy stored to the gases flowing in through delivery pipe 6. The layout of the embodiment described above, with its rotating crown provided with a catalytic bed and a heating load arranged concentrically allows, in relation to prior embodiments, to obtain a decrease in the global volume between 8 % and 27 % and in the weight of material between 6 % and 32 %, according to the hourly flow of effluents treated (between 3,000 m; and 130,000 m3). Similarly, still according to the hourly flow, the volume of catalyst that can be loaded can be increased by 20 to 60 %. These variations have a considerable effect on the costs. Tests carried out for a pilot installation capable of treating 3,000 m;/h of air polluted by xylene produced the results as follows : - heat efficiency 95 % - limit rate allowing an autothermal catalytic oxidation 0.6 g/Nm; - cleaning efficiency 99.2 % W^ CLAIM: 1. A rotating catalytic cleaning device for gaseous effluents having polluting substances, comprising a hums or cage (2) with a central part, a crown (I) located within the cage and motive means for driving the crown into a continuous rotating motion around a vertical axis (3), at least one delivery pipe (6) for feeding effluents into cage (2) and at least one pipe (7) for discharging effluents out of the cage crown (1) comprising at least a first in flow sector (Zl) for continually communicating said delivery pipe (6) with the central part (11) of cage (2), and at least a second outflow sector (Z2) of the crown for continually communicating said central part (11) of the cage wilt the discharge circuits and a catalytic cleaning reactor (R) for burning the polluting substances mixed with the effluents channelled by said first inflow sector, characterized in that it comprises in combination at least an annular rotating catalytic bed (9) arranged in the aimer part of said crown (i) on tile total circumference thereof and a rotating load (M) of a material exhibiting a large heat exchange surface arranged in the crown, outside said catalytic bed (9). 2. The device as claimed in claim 1, wherein said crown (1) is eccentric in the cage (2), the latter delimiting around the crown two peripheral zones (Za, Zb) of variable section, and two intermediate zones of high pressure drop so as to prevent parasitic flows from bypassing thermal reactor (R). 3. The device as claimed in any one of claims 1 or 2, wherein insulating joints (12) are provided between the cage (2) and the crown (1). 4. The device as claimed in any one of the preceding claims, wherein the cleaning reactor (R) comprises heating means communicating with the central zone of the crown. 5 The device as claimed in claim 4, wherein a fresh gas delivery pipe (16) is disposed in the central zone (11) of crown (1), said heating means comprising a burner (B) arranged in said delivery pipe (16). 6, The device as claimed in claim 4 or 5, wherein the heating means comprises an outer burner (B) arranged above the central zone (11) of crown (I). 7 The device as claimed in claim 6, wherein means for injecting a flow of temperature regulating fresh gas into an intermediate zone between the inflow and the outflow zones (Zl, Z2) are provided, 8. The device as claimed in any one of the preceding claims, wherein the crown has inner separating (8) for splitting up the crown into several angular zones, each of these angular zones being filled, outside the catalytic bed, with said load (M) in the form of a bulk load. 9. The device as claimed in any one of claims 1 to 7, wherein the crown comprises a plurality of parallelepiped chambers (10) intended to contain said load (M) exhibiting a large heat exchange surface. 10. The device as claimed in any one of claims 8 or 9, wherein said load (M) exhibiting a large heat exchange surface consists of knitted, woven or needled metal mats. 11. The device as claimed in any one of claims 8 or 9, wherein said load (M) exhibiting a large heat exchange surface consists of stone blocks. 12. The device as claimed in any one of claims 8 or 9, wherein said load (M) exhibiting a large heat exchange surface consists of a honeycomb structure. 13. The device as claimed in any one of claims 8 or 9, wherein said load (M) exhibiting a large heat exchange surface is made from turning or machining chips. 14. The device as claimed in any one of the preceding claims, wherein the crown (1) and the cage (2) comprise each an upper end part and a lower end part, and seal elements arranged between the corresponding upper and lower walls. 15. The de\Taco as claimed in any one of the preceding claims, wherein means for injecting a flow of sweep gas into an intermediate zone between the inflow and the outflow zones (Za, Zb) are provided. 16. A rotating catalytic cleaning device for gaseous effluents having polluting substances substantially as herein described with reference to the accompanying drawings.

Full Text

The invention relates to a rotating catalytic cleaning device for gaseous effluents having polluting substances suited for working as a heat exchanger and as a thermal and/or catalytic effect cleaner.
The invention notably applies to heat exchange systems or to systems suited for cleaning air loaded with substances such as volatile organic compounds (VOC), that can be oxidized and eliminated by thermal or catalytic incineration.
THE OF THE INVENTION
The claimant's patent application 94 06,282 describes a heat exchange and thermal and/or catalytic effect cleaning device for polluted gases such as Voss. It comprises a housing or cage, a crown containing a load of solid particulate materials selected because they exhibit a large heat exchange surface (silica, granite or Günter materials such as metallic honeycomb structures or others, or cryogenic nodules for negative temperatures, etc) that is placed in the depth of the cage. The crown is split up into several parts by an inner separation or, in some cases, it serves as a support for a certain number of baskets. Motive means are used for driving the crown and the cage into a rotating motion in relation to one another about a vertical axis (either the crown rotates, the cage being stationary, or the crown is stationary and the cage rotates about it).

The prior device comprises a pipe for delivering effluents into the cage and I pipe for discharging effluents out of the cage. The crown comprises a first ector for communicating continually the delivery pipe with the central part of he cage where a first heat exchange occurs between the effluents and the load n the crown. By means of a second sector of the crown where a second heat exchange takes place between effluents and the load in the crown, the central >art of the cage communicates continually with the discharge pipe.
This prior device can be used only as a simple heat exchanger or for a combined use as a heat exchanger and as an incinerator for polluted effluents. In [lies case, the delivery pipe receives effluents containing polluting substances, 'he first sector and the second sector communicate directly with one another by leans of the central part of the cage. A thermal reactor possibly provided with a atalytic bed selected to bring about an exothermic reaction in the presence of le polluting substances is placed in this central part in order to burn the polluting substances in the effluents channeled by the first angular sector.
With this layout, the crown rotates between two stationary parts : the entrap reactor and the housing. In order to prevent leaks due to the bypassing f the central zone reactor, it is necessary to provide a double annular seal. This ; obtained by imposing tight shape and concentricity tolerances during the manufacturing stage as well as during the mounting stage.
SUMMARY OF THE INVENTION
The rotating catalytic cleaning device for polluted gaseous effluents according to the invention comprises a housing or cage, a crown placed in the

cage, and motive means for driving the crown into a continuous rotating motion with respect to the cage about a vertical axis, at least one pipe for delivering effluents into the cage and at least one pipe for discharging effluents out of the cage, the crown comprising at least a first sector for communicating continually the delivery pipe with the central part of the cage, and at least a second sector for communicating continually the central part of the cage with the discharge circuits and a catalytic cleaning reactor for burning the polluting substances mixed with the effluents channeled by the first angular sector.
The device is characterized in that it comprises in combination at least an annular catalytic bed arranged in the inner part of the crown over the total circumference thereof and a load of a material exhibiting a large heat exchange surface arranged in the crown, outside the catalytic bed.
With this layout, the polluted effluents (possibly preheated in an outer exchanger), after heating up in contact with the thermal mass in the outer part of the first angular sector of the crown, are cleaned by crossing a first time the annular catalytic bed covering the inner wall of the crown. They cross the bed a second time on the other side of the central part, before they yield part of the heat acquired by means of the catalytic incineration to the thermal mass in the second angular sector of the crown prior to their discharge.
This layout of the mass having a large heat exchange surface and of the catalyst in the rotating part of the device allows the weight and the volume of the crown to be decreased, which simplifies its design. It also facilitates its assembly and lowers manufacturing and maintenance costs.

The crown being within the cage, two bearings are sufficient to support its shaft and to bear the stresses. To drive it into rotation, outer motive means sufficiently distant from the warmest zones can be used and installed on top of the device, which allows its headroom to be decreased.
The thickness of the catalytic bed is selected sufficient for the polluted gases to be cleaned after their two successive passages through the catalytic bed, on either side of the central part.
The thermal reactor preferably comprises heating means communicating with the central zone of the crown, such as a burner arranged in a fresh effluent delivery pipe opening into the central zone of the crown or a burner placed outside the crown, above its central zone, and preferably associated in this case with means for injecting a flow of temperature regulating fresh gas into an intermediate zone between the inflow and the outflow zones.
With this combination of effluent cooling and heating means, the incineration temperature can be easily regulated when it varies on account of the variation in the proportion of polluting substances in the effluents.
This addition of a burner is most often necessary for starting if the polluted gases delivered are not warm enough or if the VOC proportion in the gases is not sufficient for the self-containment of the exothermic reaction in the reactor.
According to an embodiment, the crown is eccentric in the cage, the latter delimiting around the crown two peripheral zones of variable section, and two intermediate zones of high pressure drop so as to prevent parasitic flows from

bypassing the thermal reactor, and insulating joints can be provided between the cage and the crown.
According to an embodiment, the crown is split up into several angular zones by an inner separation (8), each of these zones being filled, outside the catalytic bed, with a bulk load of a material having a large heat exchange surface. The crown can also comprise a plurality of parallelepiped chambers containing the load exhibiting a large heat exchange surface.
This load exhibiting a large heat exchange surface consists for example of knitted, woven or needled metallic mats, stone blocks, a honeycomb structure or it is made from turning or machining chips.
The crown and the cage comprise each an upper end part and a lower end part, and preferably seal means arranged between the corresponding walls, such as blade joints or flap joints. The upper and lower seal is easy to provide because the temperature is relatively low therein.
The device can also comprise means for injecting a flow of sweep gas into an intermediate zone between the inflow and the outflow zones.
The continuous cleaning process according to the invention is characterized in that it comprises establishing a permanent circulation of effluents to be cleaned on one hand between delivery pipes and on the other hand discharge pipes through a rotating crown provided with an inner separation and containing at least an annular catalytic bed arranged against its inner wall and a load of a material exhibiting a large heat exchange surface

Co
arranged in the crown outside titer catalytic bed, so that the effluents flow through the rotating load and heat up in contact therewith in a first heat exchange zone and, after a double passage through the rotating catalytic bed and incineration, in that they heat the thermal mass in a second heat exchange zone.
With the process according to the invention, the polluting substances can be incinerated at a temperature of the order of 400 to 500°C only, which simplifies the design and reduces technical constraints, as well as the manufacturing cost.

.Accordingly, the present invention provides a rotating catalytic cleaning device for
gaseous effluents having polluting substances, comprising a housing or cage with
a central part, a crown located within the cage and motive means for driving the
crown into a continuous rotating motion around a vertical axis, at least one
delivery pipe for feeding effluents into cage and at least one pipe for desiring
effluents out of the cage, crown comprising at least a first in flow sector for
continually communicating said delivery pipe with the central part of cage, and at
least a second outflow sector of the crown for continually communicating said
central part of the cage with the discharge circuits and a catalytic cleaning reactor
for burning the polluting substances mixed with the effluents channelled by said
first inflow sector, characterized in that it comprises in combinaticm at least an
p- annular rotating catalytic bed arranged in the inner part of said crown on the total
O circumference thereof and a rotating load of a material exhibiting a large heat

exchange surface arranged in the crown, outside said catalytic bed

Other features and advantages of the improved device according to the invention will be clear from reading the description hereafter given by way of non limiting example, with reference to the accompanying drawings in which :
- Figure 1 diagrammatically shows a cross-section of an embodiment of the device, in a combined use as an incinerator for polluting substances in effluents and as a heat exchanger, and
- Figure 2 shows an embodiment variant of the means for regulating the temperature of the catalytic reactor.

DESCRIPTION OF THE PREFERRED EMBODIMENTS
The device comprises (Figure 1) a drum consisting of a crown (1) of vertical axis arranged in a metallic outer housing or cage 2 of centrically shape for example. The diameter of the cage or housing 2 is greater than that of crown 1. The latter is offset with respect to cage 2. On either side of the diametral plane containing the vertical axis 3 of the crown, and along a Emitted angular sector, cage 2 comprises a portion of a lateral wall 4 substantially tangent to the lateral wall 5 of the crown. The inner space of the cage around crown 1, on either side of wall portion 4, thus comprises two rounded zones of variable section Za and Zb. They communicate respectively with a pipe 6 intended to deliver the gaseous effluents to be cleaned and with a pipe 7 intended to discharge these effluents after cleaning.
Crown 1 is provided with an inner separation consisting of evenly distributed straight radial plates 8. A first angular sector Zl delimited by one or several of these radial plates 8 channels the effluents to be cleaned and fed into the convergent zone Za towards the central zone 11 of the crown (flow Fe). A second angular sector Z2 communicates the central zone 11 of the crown with the divergent zone Zb and with discharge pipe 7 (flow Fs).
The inner wall of the crown is entirely covered with an annular catalytic bed 9 that the effluents must cross to reach the reactive central zone 11. This catalytic bed 9 consists either of a particle bed, or preferably of a honeycomb catalyst, which allows, all other things being equal, to reduce its thickness and volume, and especially to decrease the pressure drop it generates.

An active mass M consisting of a material having a large heat exchange surface is arranged in the remaining part of the crown outside this catalytic bed, between the separation plates 8. It can be ceramic or metal balls, turning or machining chips, a bulk or structured packing, a honeycomb structure with regular or irregular cells such as honeycombs, knitted, woven or needled metallic mats, etc. A honeycomb structure such as that described in the claimant's patent FR-2,564,037 is advantageously used. This mass exhibiting a large heat exchange surface can also consist of stones.
In order to facilitate manufacturing and loading, the crown can also be so arranged that it serves as a support for a certain number of parallelepipedic baskets 10 separate from one another, as shown in Figure 1.
In the diametral plane containing the axis 3 of crown 1, the narrowness of the space remaining between the crown and cage 2, on account of its eccentricity and of wall projection 4, generates a pressure drop sufficient to prevent direct peripheral communications between the two upstream and downstream spaces Za and Zb other than through the central zone 11. Joints or flap joints 12 can be possibly placed on the periphery of the crown where the temperature is relatively low in order to complete the seal.
The crown and the cage are closed at their lower and upper parts by even plates 13. Several blade joints (not shown) simultaneously resting between the corresponding plates of the crown and of the cage prevent parasitic bypassing flows between zones Za and Zb.

Motive means (not shown) arranged above the cage for example are coupled with the shaft 3 of the crown for driving it into rotation with respect to cage 2.
The intermediate angular sector delimited by the wall portion 4 of the cage preferably comprises a pipe 14 for injecting fresh air intended to blow off the foul effluents through the thermal mass and the catalyst in the few angular sectors of the crown passing before it, prior to each inversion of the direction of flow. After crossing the drained sectors, the sweep air mass reaches the central zone 11 where it is carried along with the main flow towards zone Zb through crown 1.
In the angular sector opposite pipe 14, the cage comprises another pipe 15 (Figure 1) for injecting fresh air intended to regulate possibly the temperature of the catalytic reaction if it rises too much.
The reaction that takes place in the central zone is exothermic and it is adjusted so as to release enough energy to compensate substantially for the calorific dissipation. A proportion of 0.4 g of VOC per m; of effluents is enough for an autothermal running.
A burner (B) supplied with natural gas or LPG is arranged above central zone 11 for example, its flame entering directly the central zone. It is used to heat the incoming flows at the starting point if necessary, so as to reach an autothermal working point, or possibly to provide makeup heat if the polluting compounds VOC content is insufficient to obtain an autothermal running.

According to the embodiment of Figure 1, the temperature in the catalytic reactor is controlled separately by means of a burner B above the crown and of a radial pipe 15 delivering fresh effluents.
According to the embodiment of Figure 2, burner B can be placed in a pipe 16 opening into central zone 11 instead of being placed directly above this zone. Pipe 16 can act as a bypass line connected to the pipe 6 delivering the effluents to be treated. The flow diverted through this pipe 16 is controlled by a valve VI. Burner B is supplied with fuel by means of a control valve V2. By varying the flow of effluents diverted through pipe 16 and its temperature by means of burner B, the exothermic reaction can be controlled in the reactor. If the polluting substances concentration exceeds the autothermal limit, cold effluents are injected. On the other hand, the burner is fed if this concentration remains below this limit and during the installation starting period.
After their double passage through the catalytic bed, on either side of central zone 11, the polluting compounds (VOC) are converted by the reaction into various combustion products : CO2, H2O, N2 mainly, SOx and NO; as
traces.
The high temperature gases coming from the reactive zone flow through the part of the load M located in the angular zone Z2 of the crown and they yield a good part of their calories thereto. The rotation of crown 1 with respect to cage 2 progressively brings the heated elements towards the angular zone Zl where they can yield in turn part of the calorific energy stored to the gases flowing in through delivery pipe 6.

The layout of the embodiment described above, with its rotating crown provided with a catalytic bed and a heating load arranged concentrically allows, in relation to prior embodiments, to obtain a decrease in the global volume between 8 % and 27 % and in the weight of material between 6 % and 32 %, according to the hourly flow of effluents treated (between 3,000 m; and 130,000 m3). Similarly, still according to the hourly flow, the volume of catalyst that can be loaded can be increased by 20 to 60 %. These variations have a considerable effect on the costs.
Tests carried out for a pilot installation capable of treating 3,000 m;/h of air polluted by xylene produced the results as follows :
- heat efficiency 95 %
- limit rate allowing an autothermal catalytic oxidation 0.6 g/Nm;
- cleaning efficiency 99.2 %

W^ CLAIM:
1. A rotating catalytic cleaning device for gaseous effluents having polluting substances, comprising a hums or cage (2) with a central part, a crown (I) located within the cage and motive means for driving the crown into a continuous rotating motion around a vertical axis (3), at least one delivery pipe (6) for feeding effluents into cage (2) and at least one pipe (7) for discharging effluents out of the cage crown (1) comprising at least a first in flow sector (Zl) for continually communicating said delivery pipe (6) with the central part (11) of cage (2), and at least a second outflow sector (Z2) of the crown for continually communicating said central part (11) of the cage wilt the discharge circuits and a catalytic cleaning reactor (R) for burning the polluting substances mixed with the effluents channelled by said first inflow sector, characterized in that it comprises in combination at least an annular rotating catalytic bed (9) arranged in the aimer part of said crown (i) on tile total circumference thereof and a rotating load (M) of a material exhibiting a large heat exchange surface arranged in the crown, outside said catalytic bed (9).
2. The device as claimed in claim 1, wherein said crown (1) is eccentric in the cage (2), the latter delimiting around the crown two peripheral zones (Za, Zb) of variable section, and two intermediate zones of high pressure drop so as to prevent parasitic flows from bypassing thermal reactor (R).
3. The device as claimed in any one of claims 1 or 2, wherein insulating
joints (12) are provided between the cage (2) and the crown (1).
4. The device as claimed in any one of the preceding claims, wherein the
cleaning reactor (R) comprises heating means communicating with the
central zone of the crown.

5 The device as claimed in claim 4, wherein a fresh gas delivery pipe (16) is disposed in the central zone (11) of crown (1), said heating means comprising a burner (B) arranged in said delivery pipe (16).
6, The device as claimed in claim 4 or 5, wherein the heating means comprises an outer burner (B) arranged above the central zone (11) of crown (I).
7 The device as claimed in claim 6, wherein means for injecting a flow of temperature regulating fresh gas into an intermediate zone between the inflow and the outflow zones (Zl, Z2) are provided,
8. The device as claimed in any one of the preceding claims, wherein the crown has inner separating (8) for splitting up the crown into several angular zones, each of these angular zones being filled, outside the catalytic bed, with said load (M) in the form of a bulk load.
9. The device as claimed in any one of claims 1 to 7, wherein the crown comprises a plurality of parallelepiped chambers (10) intended to contain said load (M) exhibiting a large heat exchange surface.
10. The device as claimed in any one of claims 8 or 9, wherein said load (M) exhibiting a large heat exchange surface consists of knitted, woven or needled metal mats.
11. The device as claimed in any one of claims 8 or 9, wherein said load (M) exhibiting a large heat exchange surface consists of stone blocks.
12. The device as claimed in any one of claims 8 or 9, wherein said load (M) exhibiting a large heat exchange surface consists of a honeycomb structure.
13. The device as claimed in any one of claims 8 or 9, wherein said load (M) exhibiting a large heat exchange surface is made from turning or machining chips.

14. The device as claimed in any one of the preceding claims, wherein the
crown (1) and the cage (2) comprise each an upper end part and a lower end
part, and seal elements arranged between the corresponding upper and
lower walls.
15. The de\Taco as claimed in any one of the preceding claims, wherein means
for injecting a flow of sweep gas into an intermediate zone between the
inflow and the outflow zones (Za, Zb) are provided.
16. A rotating catalytic cleaning device for gaseous effluents having polluting
substances substantially as herein described with reference to the
accompanying drawings.