EP0440181A2 - Réacteur à régénération pour brÀ»leur des effluents gazeux industriels - Google Patents

Réacteur à régénération pour brÀ»leur des effluents gazeux industriels Download PDF

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Publication number
EP0440181A2
EP0440181A2 EP91101187A EP91101187A EP0440181A2 EP 0440181 A2 EP0440181 A2 EP 0440181A2 EP 91101187 A EP91101187 A EP 91101187A EP 91101187 A EP91101187 A EP 91101187A EP 0440181 A2 EP0440181 A2 EP 0440181A2
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EP
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Prior art keywords
gas
heat exchanger
reactor according
reactor
oxidation chamber
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Granted
Application number
EP91101187A
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German (de)
English (en)
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EP0440181B1 (fr
EP0440181A3 (en
Inventor
Bernhard Dipl.-Ing. Mokler
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LTG Lufttechnische GmbH
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LTG Lufttechnische GmbH
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • F23G7/07—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases in which combustion takes place in the presence of catalytic material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • F23G7/061—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating
    • F23G7/065—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel
    • F23G7/066—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel preheating the waste gas by the heat of the combustion, e.g. recuperation type incinerator
    • F23G7/068—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel preheating the waste gas by the heat of the combustion, e.g. recuperation type incinerator using regenerative heat recovery means

Definitions

  • the invention relates to a regenerative reactor for burning industrial exhaust gases, in particular exhaust air containing pollutants, according to the preamble of claim 1. Furthermore, the invention relates to a method for burning industrial exhaust gases according to the preamble of claim 16.
  • Such a reactor system with three reactors in the form of so-called treatment towers is known from DE-OS 37 37 538.
  • these towers are connected by a large-volume connecting line.
  • this must be brought to the oxidation temperature when starting, which can be, for example, 800.degree. This requires considerable amounts of heat and long heating times.
  • a similarly constructed reactor system is known from DE-OS 38 37 989. No separate treatment towers are provided for this. Rather, three heat exchangers are arranged in a row next to one another within a housing. Here, too, there is a very large oxidation chamber, which at the same time also creates the connection between the heat exchangers. This oxidation chamber must first be heated when starting, which requires a lot of energy and long heating times. moreover, due to the high operating temperature, high heat losses occur.
  • a method for the treatment of a gas for the removal of impurities in which a reactor called a furnace is used, which has a cylindrical housing which has three heat exchanger regions which are sector-shaped in cross section. There is an oxidation chamber above the heat exchanger areas, in which the exhaust gases are burned. Due to the heat generated, the housing is subjected to high mechanical loads, which can lead to deformation or even destruction.
  • a reactor is preferred in which the expansion compensation zone of the partitions extends over the entire wall Width extends and the partitions are corrugated.
  • Partition walls designed in this way can absorb forces over their entire width and thus reduce stresses which occur when the reactor heats up excessively.
  • the partitions are relatively simple and therefore inexpensive to manufacture.
  • an embodiment of the reactor is particularly preferred in which the partition walls are double-walled. Since the adjacent heat exchanger areas are exposed to different gas flows and thus have different temperatures, thermal stresses which are based on the sharp drop in temperature within the partition walls can be reduced.
  • the double-walled walls isolate the individual heat exchanger areas better from each other, so that less thermal stresses can occur.
  • an embodiment of the reactor is preferred in which the partition walls starting from the peripheral wall meet at one point and are connected to a double-walled tube.
  • This opens on the one hand in the oxidation chamber of the reactor and on the other hand outside the housing. It is therefore possible to extract hot gas from the oxidation chamber and thus optimally adjust the temperature of the reactor, in particular to avoid overheating. In this way, an excessive increase in temperature inside the reactor can be avoided. This can also cause thermal stress optimally dismantle.
  • air preferably cold air, can be supplied to the gas withdrawn from the oxidation chamber, so that the gas withdrawn from the reactor overall has a significantly lower temperature than in the oxidation chamber. This also makes it possible to further reduce thermal loads on the reactor and the downstream elements.
  • An exemplary embodiment of the reactor is particularly preferred, which is characterized in that a flap is arranged in the tube serving to draw off the gas and can be acted upon by the withdrawn gas and the cold air supplied. Due to the reduced gas temperature due to the supply of cold air, the thermal load on the flap decreases, which can then be carried out relatively easily.
  • the object of the invention is also to provide a method for burning industrial exhaust gases, in particular pollutant-containing exhaust air, in which the thermal load on the reactor is minimized.
  • a method is particularly preferred in which hot clean gas, hot gas, is withdrawn from the oxidation chamber when the temperature inside the reactor threatens to become too high.
  • Fresh air preferably cold air, is added to the hot gas to reduce the thermal load on downstream control means.
  • FIG. 1B shows the base part of a regenerative reactor 10 with a circular cylindrical peripheral wall 11.
  • a tube 12 extends in its longitudinal axis and projects beyond the upper edge R 'of the peripheral wall 11.
  • three partitions 13, 14 and 15 are welded, which are arranged at equal angular intervals of 120 ° and have the same shape. If more than three partitions are provided, the angular distances should be selected accordingly.
  • the partitions are designed as rectangles, a cutout 13 ', 14' or 15 'being provided at the upper, inner corner facing the tube 12, which extends obliquely upwards and outwards from the upper end of the tube 12 , as can be seen from Figures 1B and 8.
  • the boundary line of the section can, for example — as in FIG. 1B — run in the shape of a sector of a circle but also linearly.
  • the peripheral wall 11 is closed at the bottom by a bottom which seals the housing in a gastight manner.
  • the partitions 13, 14 and 15 extend to this floor and are welded to it.
  • the interior of the housing is divided into three circular sector-shaped areas 1, 2 and 3, which are gas-tightly separated from one another by the partition walls, but in the upper area, namely in the area of the cutouts or cutouts 13 ', 14 'and 15' are connected.
  • each of the areas 1, 2 and 3 has the index number of the area in question.
  • Each of the areas in the floor 17 thus has a connection opening A for raw gas, which is consequently designated A1, A2 and A3.
  • each area 1, 2 and 3 has a connection opening R for clean gas, which is correspondingly designated R1, R2, for example R3.
  • each of the areas 1, 2 and 3 has a connection opening S for purging gas, which is correspondingly designated S1, S2 and S3.
  • connections for raw gas (A1 to A3), clean gas (R1 to R3) and purge gas (S1 to S3) can each be provided directly with a valve or slide, as is indicated in FIG. 2 by the oblique lines 25.
  • valves or slides can be located in the feed lines to these connections.
  • Such valves are usually designed as flaps.
  • an inflow chamber enclosed by the peripheral wall 11 is formed within the housing, which is separated into gas-tight inflow chambers by the three partition walls 13, 14 and 15 AK1, AK2 and AK3 is divided.
  • the inflow chambers extend from the bottom 17 to a grate 30 approximately over a third of the height of the interior of the housing.
  • the grate 30, which can be designed as the grate 30 'shown in section in FIG. 4 and which is only indicated schematically in FIG. 1B, serves to support a bed 35 made of inert ceramic material with high heat storage capacity, which differs from the grate 30 extends almost to the upper edge R 'of the peripheral wall 11.
  • the fill is indicated by cross hatching 36 in FIG. 1B.
  • the temperature of the bed in the area of this cross-hatching decreases from top to bottom, for example a temperature of approximately 700 ° C. to 800 ° C. above and a temperature of approximately 100 ° C. below.
  • annular flange 40 is attached to the outside of the peripheral wall 11, which is provided with holes 41 in a conventional manner.
  • This ring flange is therefore located in a medium temperature zone of, for example, 300 ° C. Depending on whether the flange is attached further up or down, the temperature prevailing there changes.
  • a ring flange 45 of a hood-shaped part is fastened to the ring flange 40, which is referred to below as hood 47 and is shown in FIG. 1A.
  • This ring flange 45 also has holes 46, which can be brought into alignment with the holes 41 in the ring flange and serve to accommodate screws or other fastening means. With the help of these screws, not shown here, the hood can be attached to the housing.
  • the hood 47 has a cylindrical section 49 adjoining the ring flange 45, which is preferably made of steel and merges into a circular cover 50 at the top, which can also be made of steel and forms the upper end of the hood 47.
  • the embodiment of the reactor shown here is circular-cylindrical, that is to say that the housing, like the hood 47, has a circular-cylindrical shape. It is also conceivable that both parts are triangular, the triangular shape of the housing or the hood then being predetermined by triangular areas of the heat exchanger. Instead of the triangular shape, other polygonal outer shapes of the housing or the hood can also be selected.
  • the hood 47 is continuously provided with a refractory lining, which is only indicated schematically here with the reference number 52.
  • the material of the lining can be chosen arbitrarily.
  • a fireproof brick with lightweight bricks, with fireproof cement or with a fireproof mat made of silicates, for example, can be selected.
  • peripheral wall 11 and the partition walls 13, 14 and 15 do not have to be lined with fire-resistance.
  • the use of high-alloy steel is sufficient here.
  • the insulation in the upper, particularly hot region of the bed 35 is taken over by the refractory lining 52 of the hood 57.
  • the hood 47 has a lateral connection piece 55, through which hot gas can be removed, for example for heating water, if necessary, for example if the heat generated during the combustion of the raw gas is too high. Likewise, hot gas can also be withdrawn through the central tube 12, which results in a particularly compact construction of the reactor.
  • a burner 56 is provided on the hood 47, which can be arranged in the cover 50, or as shown here, in the side wall of the hood. The flame of the burner is directed towards the center of the space enclosed by the hood 47.
  • the inside diameter of the hood 47 is dimensioned such that only a small gap 51 (see FIG. 8) remains between its inside and the radial outside 13 ′′, 14 ′′ and 15 ′′ of the partitions 13, 14 and 15.
  • the height of the hood 47 is dimensioned such that only a small gap 53 (see FIG. 8) remains between its inside in the area of the cover 50 and the upper edge 13 ′′ ′′, 14 ′′ ′′ and 15 ′′ ′′ of the partition walls.
  • an oxidation chamber 60 of the reactor 10 is formed between its inner wall and the top of the bed 35, in which the main oxidation of the raw gas supplied takes place.
  • raw gas, clean gas and purge gas are alternately routed through the various heat exchanger areas.
  • the raw gas is fed through the bed 35 in the heat exchanger area 1 of the oxidation chamber 60 and burned there.
  • the resulting clean gas is discharged through the bed 35 in the heat exchanger area 2.
  • the gas in the oxidation chamber 60 must flow from the oxidation chamber area O1 above the heat exchanger area 1 through the recesses 13 ', 14' and 15 'of the partition walls 13, 14 and 15. There is an intensive swirling. This area of the cutouts in the partition walls is therefore also called the swirl area VW.
  • the air in the swirl region VW is heated by the burner 56 and brought to the reaction temperature.
  • the burner must also be switched on if the heat released during the combustion of the exhaust gases is not sufficient to maintain the reaction temperature.
  • the gas flow is adjusted by adjusting the slide or flaps, the connections for raw gas (A1 to A3), clean gas (R1 to R3) and purge gas (S1 to S3) are assigned. It does not matter through which heat exchanger area the raw gas is supplied and through which the clean gas is discharged. Due to the symmetry of the arrangement, the same relationships always result.
  • FIG. 2 schematically shows the pipelines connected to the reactor 10 and the associated valves or flaps.
  • the raw gas is supplied to the connections A1, A2 and A3 and the valves arranged there to the reactor via a line 62, into which a blower 63 or some other air delivery device can optionally be connected.
  • the clean gas can be drawn off or sucked from the connections R1, R2 and R3 into a line 65 by a blower 64 or another air delivery device and fed via a line 66, for example to a chimney, or via a line 20 and a line 67 as purge gas to the connections S1 up to S3.
  • dashed lines of the blower 63 is intended to indicate that one of the blowers can also be omitted.
  • a dashed line in FIG. 2 indicates that air or cold air can also be used as a purge gas via a line 21.
  • the heat exchanger regions of the reactor 10 are identified by the numbers 1, 2 and 3.
  • An upward-pointing arrow indicates that the temperature of the bed 35 of the relevant heat exchanger area is increasing, while a downward-pointing arrow means that the temperature of the relevant bed 35 of this area is decreasing.
  • a horizontal line indicates that the temperature of the bed remains essentially unchanged.
  • connection A1, R2 and S3 are initially opened in phase I, so that raw gas is fed via the bed 35 in the heat exchanger area 1 to the oxidation chamber 60 and is oxidized there.
  • This process is exothermic, which means that heat is released.
  • the resulting hot gas is discharged as clean gas via the bed 35 in the heat exchanger area 2.
  • the bed 35 in the heat exchanger area 3 is flushed with purging gas.
  • the heat exchanger area heated by the clean gas is used for heating the raw gas supplied, which may be present there can also ignite and thus be oxidized.
  • Version 2 of the method shown in FIG. 3 is more effective, but involves a higher switching effort: Rinsing phases IIa, IIIa and Ia, which for example each lie between phases Ib, IIb and IIIb, which last, for example, 2 to 3 minutes Last 10 seconds, and during which raw gas is flushed from a heat exchanger area into the oxidation chamber and burned there.
  • the connections A1, R2 and R3 are opened in version 2 during phase Ib, so that raw gas is supplied to the oxidation chamber 60 via the heat exchanger area 1, oxidized there and then discharged again via the two heat exchanger areas 2 and 3 connected in parallel .
  • the latter are heated up while the heat exchanger area 1 releases heat to the raw gas and thereby becomes colder.
  • the heat exchanger area 1 is briefly flushed during phase IIa in order to burn the raw gas still contained in it in the oxidation chamber 60.
  • the raw gas is otherwise supplied to the oxidation chamber 60 through the heat exchanger area 2 during phase IIa and derived from there as clean gas via the heat exchanger area 3.
  • the clean gas is then additionally discharged via the -purged- heat exchanger area 1 in phase IIb.
  • the further process of the cyclical interchange is shown in FIG. 3, version 2. That is, the supply and discharge of raw and clean gas or of purge gas is continued, as just described, in each case in the subsequent heat exchanger area.
  • FIG. 4 shows very schematically a simplified system with only two heat exchanger areas 70 and 71, in which there is also a bed 35 of heat exchanger material.
  • the heat exchanger regions 70 and 71 each have a semicircular cross section here, which results from FIG. 6.
  • the beds 35 lie on a grate 30 ', to which an inflow chamber or an inflow box 72 or 73 adjoins at the bottom.
  • the connections of the inflow box 72 are designated A1, S1 and R1, those of the connection box 73 with A2, S2 and R3, the connection openings A being determined for raw gas, the connection openings R for clean gas and the connection openings S for purge gas.
  • the partition between the two heat exchanger areas 70 and 71 and the two inflow boxes 72 and 73 is designated 74. It has a flow opening 75 at the top in the oxidation chamber 76, which is shown in FIG. 7 and essentially here is rectangular. A gas stream 77 can flow through this opening from left to right or a gas stream 78 from right to left, which is indicated in FIG. 4 by corresponding arrows.
  • the flame of an ignitable burner 56 ' is directed at the flow opening 75.
  • a line 80 is laterally connected to the oxidation chamber 76, in which a valve B designed as a flap is arranged.
  • Line 80 is required for the rinsing processes which take place during phases Ib and IIb according to FIG.
  • the feed line for raw gas is designated in FIG. 4 with 82, the discharge line for clean gas with 83. It usually leads to a chimney, not shown here.
  • the feed line for purge gas is designated 84.
  • the reactor 85 shown in FIG. 4 can be constructed similarly to the reactor 10 according to FIGS. 1A and 1B.
  • a hood with refractory lining can also be provided here, which can also be welded to the peripheral wall 11 '.
  • the hood is not shown in FIGS. 4 to 7, since these figures only show a schematic representation.
  • phase Ia The gas flow 77 in the oxidation chamber 76 indicated by an arrow arises in phase Ia, that is to say when the connections A1 and R2 are open are. For example, these remain open for 3 minutes.
  • phase Ib the heat exchanger area 70 is flushed by opening the connection S1, the flushed gas after combustion in the oxidation chamber 76 being fed directly to the chimney via the line 80 and the valve B.
  • phase IIa the gas stream 78 indicated by an arrow being formed while the connections A2 and R1 are open. It is then rinsed in accordance with phase IIb. Afterwards, phase Ia is started again.
  • FIG. 4 provides blowers 63 'and 64' which push or suck the gas flows through the reactor 85.
  • FIG. 6 shows a top view of the reactor 85 shown in FIG. 4, the cover being removed.
  • peripheral wall 11 ', the burner 56' mounted in the hood of the reactor 85, the partition 74 provided with expansion compensation zones DA between the heat exchanger regions 70 and 71 and the throughflow opening 75 provided in this partition, which here forms the swirl region, can be seen.
  • the line 80, in which a valve B is located, is connected laterally to the oxidation chamber 76.
  • FIG. 7 shows a cut-open reactor 85, as shown in FIGS. 4 and 6.
  • the partition 74 can be seen from the side, so that its flow opening 75 is clearly visible. Through this one can see the opening of the burner 76, which is directed towards the throughflow opening or the swirl region of the reactor 85.
  • the two regions of the oxidation chamber 76 which are separated from one another by the partition 74 are connected to one another via the flow opening 75.
  • FIG 8 shows a partial section through a reactor 10, as shown in Figures 1A and 1B.
  • the hood 47 is placed on the housing of the reactor 10 formed by the surrounding wall 11.
  • the central tube 12 can be seen, to which the partitions 13, 14 and 15, here the partition 14, are welded.
  • the other side of the partition walls is welded to the surrounding wall 11.
  • the partitions are essentially rectangular, a recess 14 'being provided at their inner upper corner, which here has an arcuate boundary line.
  • the upper edge R 'of the housing or the surrounding wall 11 is shown in broken lines here.
  • the bed 35 of the heat exchanger region 2 is highlighted by hatching.
  • the hood 47 rests with its flange 45 on the flange 40 attached to the surrounding wall 11 and is fastened in a suitable manner, for example by screws.
  • the wall of the hood has a refractory lining 52.
  • the inner dimensions of the hood 47 are matched to the dimensions of the partition walls or the peripheral wall 11 in such a way that a gap 51 between the radial outer edge 14 ′′ of the partition wall 14 and between the upper edge 14 ′′ ′′ of the partition wall 14 and the cover 50 of the hood 47 a gap 53 remains.
  • the free space above the bed 35 is divided by the partitions 13, 14 and 15 into three areas which are connected to one another due to the cutouts 13 ', 14' and 15 '. wherein the gas flows in the area of the recesses can pass from one heat exchanger area to the other. A swirling of the gases occurs, so that this transition area is referred to as swirling area VW.
  • FIG. 9 shows any partition shown in the figures mentioned, which - seen from above - has an expansion compensation zone DA, which is U-shaped here.
  • FIG. 10 an exemplary embodiment of a partition wall is shown which, seen from above or shown in section, has an expansion compensation zone DA which is essentially S-shaped.
  • the expansion compensation zone of one of the partition walls shown in the figures extends over its entire length, the expansion compensation zone being meandering.
  • the shape of the individual meanders is of secondary importance for the function of the expansion compensation zone.
  • the individual arches of the meanders can thus be designed in the form of a circular arc or have any curvature.
  • the individual meanders can also be rectangular, trapezoidal or triangular.
  • FIG. 1 Another variant of the design of the expansion compensation zone is shown in FIG.
  • the partition is provided with several undercut areas.
  • the expansion compensation zone DA of the partition walls shown in FIGS. 9 to 12 has the function of intercepting an expansion of the partition wall based on the temperature increase.
  • the partitions are fastened on the one hand to the peripheral wall and on the other hand to the central tube inside the reactor or, as shown in FIG. 6-, in the form of a continuous partition. Also in the continuous partition of this embodiment there is an expansion or elongation of the partition based on the temperature increase, which is compensated for by the expansion compensation zone DA.
  • FIG. 13 shows - greatly simplified - the central tube 12, for example of the reactor shown in FIG. 1B.
  • the tube is double-walled here, that is, a further tube 12a is arranged inside the tube 12.
  • Both tubes end here at the same height at the lower edge of the recesses 13 ', 14' and 15 'of the partition walls 13, 14 and 15.
  • the partition wall 15 is shown as an example on the left.
  • the inner tube 12a extends concentrically to the outer tube 12 over a region. Both pipes penetrate the grate 30 on which the bed 35 of the heat exchanger areas 1 to 3 rests. They also run concentrically to one another when they pass through the bottom 17 of the housing. The inner tube 12a then describes an arc and passes through the wall of the outer tube 12.
  • the outer tube 12 has a valve or a flap K1.
  • a valve or a flap K2 is likewise provided in the tube 12a emerging from the outer tube 12.
  • FIG. 14 a schematic section through the reactor 10 is shown in FIG. 1B.
  • An inner tube 12'a which has openings indicated by arrows in its outer wall, in turn runs within the central tube 12 '. Both tubes run concentrically through the grate 30 and the bottom 17 of the housing of the reactor 10. Thereafter, the outer tube 12 'continues under an arc to a connection arranged at right angles to the tube 12', in which a flap K2 is arranged.
  • the inner tube 12'a pierces the wall of the tube 12 'in the area of the bend. Below a flap K1 is arranged in the inner tube 12'a at this breakthrough point.
  • hot clean gas can be sucked out of the swirling area VW of the oxidation chamber through the tube 12 (FIG. 13) or 12 '(FIG. 14). Hot clean gas is drawn off in particular when the temperature inside the reactor becomes too high, for example with a high solvent load on the raw gas.
  • the control of the withdrawn hot gas takes place via the flap K1 in FIGS. 12 and 13.
  • the temperature of the withdrawn hot gas is particularly high because the gas is withdrawn directly from the reaction zone.
  • the flap K1 which controls the hot gas flow is therefore particularly exposed to heat and must be made of high-quality materials.
  • the central tube of the reactor is therefore preferably of double-walled design, that is to say a central tube 12a is arranged inside the tube 12 in FIG. 13, through which cold air can be blown in, controlled by the flap K2.
  • This flows not only through the indicated openings but also from the top of the central tube 12a and is sucked with the hot gas into the annular space of the tube 12 surrounding the inner tube 12a as soon as hot gas is pulled out of the oxidation chamber after the flap K1 has been opened.
  • the cold air supplied results in a gas mixture whose temperature is significantly reduced, for example by 300 ° C., compared to the hot gas present in the oxidation chamber.
  • the one controlling the hot gas flow Flap K1 can therefore be built less complex and is therefore cheaper to manufacture. Overall, the thermal load on this area of the reactor is reduced.
  • FIG. 14 There the hot gas is drawn off through the central tube 12'a. This hot gas is controlled by the flap K1, which must be correspondingly temperature-resistant if it is acted upon directly by the hot or clean gas originating from the oxidation chamber.
  • the pipe which carries the hot gas that is to say the central pipe 12'a
  • the outer pipe 12 ' into which cold air is introduced via the flap K2
  • a reduction in the temperature due to the mixture of hot gas and cold air the flap K1 striking gas instead.
  • the temperature of the hot gas can be reduced from, for example, 800 ° C. to, for example, 500 ° C. and less.
  • the thermal load on the reactor can also be greatly reduced here, that is, a cheaper flap can be used.
  • the heat exchanger and the oxidation chamber in a round cylindrical housing, which is arranged upright.
  • the oxidation chamber is located at the upper end of this housing, the heat exchangers in the middle and the flow chambers for the heat exchangers below.
  • the resulting reactor is therefore very compact and can be heated up quickly and inexpensively.
  • the thermal loads occurring in this spatial design are reduced to a great extent by the measures described here, that is to say by the expansion compensation zones of the partition walls, by the possibility of extracting hot gas from the oxidation chamber and by the admixture of cold air.
  • the cylindrical housing is divided into sectors internally by the partitions.
  • the partitions are gas-tight and generally prevent direct gas transfer between the heat exchanger areas.
  • the upper end of the cylindrical housing forms the "hot end", that is, the oxidation chamber.
  • This is sealed off from the atmosphere by the hood 47, which can be screwed or welded to the cylindrical housing. All that is required here is a hood, which is put over the housing and radially isolating it in its hot areas by overlapping wall areas.
  • the connection point between the hood and the housing for example the flange 40 or 45 in FIGS. 1A and 1B, can be arranged such that the temperature of the wall area of the reactor is relatively low here. This means that the flange is placed approximately in the middle or somewhat below the center of the bed area 36. Therefore, the connection point is thermally relatively little stressed and can absorb the weight of the hood better, because it has a higher strength due to the lower temperature.
  • the heat exchangers consist of ceramic bulk material 35 which is heaped up on a sieve plate or a supporting grate 30, 30 '.
  • metal honeycombs could also be used.
  • the dividing walls 13 to 15 are drawn into the hood 47 via the upper edge of the heat exchanger bed in order to achieve the residence time of the hot gases in the oxidation chamber 60 or 76 which is required for the complete combustion of the substances polluting the raw gas.
  • the transition from one area of the heat exchanger to the other takes place via the cutouts or the swirl area VW. The cutouts result in a constriction of the flow, an increase in the speed of the gas flow and subsequently good mixing due to turbulence.
  • the burner 56 in the hood is arranged in such a way that the flue gas is added to the hot gas in the oxidation chamber precisely where there is a high level of turbulence and thorough mixing with the hot gas through the cutouts. Due to the symmetrical shape, when overflowing from each individual heat exchanger area to the other, the same conditions of overflow and admixing of burner flue gas can be achieved, that is to say also when the raw gas is oxidized.
  • the heat losses of the reactor are low because the circular cylindrical design has a small surface area compared to the volume.
  • the height of the reactor is therefore preferably chosen to be approximately equal to its diameter.
  • the partitions 13, 14, 15 and 74 do not necessarily need to be insulated, since the heat they transfer represents a further heat recovery.
  • the peripheral wall 11, 11 'does not have to be bricked up, since its material has no supporting function in the hot area.
  • the hood 47 can be made fireproof on the inside or insulated on the outside. Their rotationally symmetrical shape according to the figures shown here can be produced particularly inexpensively.
  • the masses to be warmed up when starting up are low, since the masses of steel, brick lining and bulk material are small and there are no dead space volumes or dead space masses. Therefore, the heating energy is low and the heating time is short.
  • the hood 47 can also have an upward-facing cavity in the area of the cutouts 13 ', 14' and 15 'or in the swirl area VW, which can also be selected to be large enough that the cutouts in the partition walls can be dispensed with.
  • the swirling of the overflowing gases takes place entirely in the bulge of the cover of the hood when the cutouts are omitted.
  • the central tube 12 then opens into this swirling area formed in the hood.
  • the lower end of the cylindrical housing is the "cold end", which acts as the flow chamber for the Heat exchanger areas can be formed (compare 72 and 73 in Figure 4 and AK1 to AK3 in Figure 1B). Other inflow areas are also possible.
  • the flow chambers have the connections A1 to A3, R1 to R3 and S1 to S3 for raw gas, clean gas and purge gas. Here valves or flaps are provided for the individual connections.
  • hot gas can be removed via the pipe 12 or the connection 55.
  • the removal is controlled by a hot gas flap 90 (FIGS. 1B and 2) or K1 (FIGS. 13 and 14), which is preferably arranged in the “cold area” or is installed in the connection 55.
  • the gases are drawn through the reactor by means of a blower 64 or pushed through by means of a blower 63.
  • the hot air line 12, 55, 80 opens into the clean gas line at the intake port of the blower 64, in the latter case in the clean gas to be removed, that is to say in the gas stream supplied to the chimney.
  • the same design of the reactor can be used for operation with a catalyst.
  • the bulk material 35 is then partially or completely replaced by catalyst bulk material or by a honeycomb catalyst.
  • the reactor then works as a catalytic combustion reactor and is very versatile.
  • the oxidation zone is wholly or partially in the heat exchanger area shifted. Since the operating temperature is lower during catalytic converter operation, appropriate design modifications can be made, for example, other materials can be used, or the wall thicknesses of the reactor can be reduced in part.
  • the reactor described here is very compact and can therefore be transported as a whole. This shortens the installation time at the place of use.

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  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
EP91101187A 1990-01-30 1991-01-30 Réacteur à régénération pour brûleur des effluents gazeux industriels Expired - Lifetime EP0440181B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE4002625 1990-01-30
DE4002625 1990-01-30

Publications (3)

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EP0440181A2 true EP0440181A2 (fr) 1991-08-07
EP0440181A3 EP0440181A3 (en) 1991-11-13
EP0440181B1 EP0440181B1 (fr) 1993-09-29

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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0548630A1 (fr) * 1991-12-20 1993-06-30 EISENMANN MASCHINENBAU KG (Komplementär: EISENMANN-Stiftung) Dispositif d'épuration d'air d'échappement nocif des installations industrielles par post-combustion régénératrice
EP0558458A1 (fr) * 1992-01-30 1993-09-01 GEICO S.p.A. Incinérateur à régénération pour l'élimination des émissions polluantes, notamment pour le traitement des émissions contenant du résidu de peinture
US5823770A (en) * 1997-02-26 1998-10-20 Monsanto Company Process and apparatus for oxidizing components of a feed gas mixture in a heat regenerative reactor
EP0780633A3 (fr) * 1995-12-20 1999-01-27 H KRANTZ-TKT GmbH Dispositif pour la combustion d'impuretés dans un courant de milieu
US5997277A (en) * 1995-12-08 1999-12-07 Megtec Systems Ab Method and a device for recovery of energy from media containing combustible substances even at low concentration
WO2009059749A3 (fr) * 2007-11-07 2009-08-20 Gerd Wurster Installation de séchage
DE102008011938B3 (de) * 2008-02-29 2009-09-10 Arge Schedler - Thalhammer Vorrichtung zur Reinigung von schadstoffhaltigem Abgas
DE102009055942A1 (de) * 2009-11-26 2011-06-01 Chemisch-Thermische Prozesstechnik Gmbh Verfahren und Vorrichtung zur Reinigung von Abgasen

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1045175B (de) * 1952-11-03 1958-11-27 Oxy Catalyst Inc Vorrichtung zur katalytischen Oxydation giftiger und schaedlicher Abgase von Brennkraftmaschinen
DE1113533B (de) * 1957-05-11 1961-09-07 Kraftanlagen Ag Regenerativ-Luftvorwaermer
DE2912304A1 (de) * 1978-03-29 1979-10-11 Nittetsu Kakoki Kk Vorrichtung zur behandlung eines gasstromes
GB2122329A (en) * 1982-06-23 1984-01-11 Regenerative Environ Equip Regenerative incinerator

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1045175B (de) * 1952-11-03 1958-11-27 Oxy Catalyst Inc Vorrichtung zur katalytischen Oxydation giftiger und schaedlicher Abgase von Brennkraftmaschinen
DE1113533B (de) * 1957-05-11 1961-09-07 Kraftanlagen Ag Regenerativ-Luftvorwaermer
DE2912304A1 (de) * 1978-03-29 1979-10-11 Nittetsu Kakoki Kk Vorrichtung zur behandlung eines gasstromes
GB2122329A (en) * 1982-06-23 1984-01-11 Regenerative Environ Equip Regenerative incinerator

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0548630A1 (fr) * 1991-12-20 1993-06-30 EISENMANN MASCHINENBAU KG (Komplementär: EISENMANN-Stiftung) Dispositif d'épuration d'air d'échappement nocif des installations industrielles par post-combustion régénératrice
EP0558458A1 (fr) * 1992-01-30 1993-09-01 GEICO S.p.A. Incinérateur à régénération pour l'élimination des émissions polluantes, notamment pour le traitement des émissions contenant du résidu de peinture
US5997277A (en) * 1995-12-08 1999-12-07 Megtec Systems Ab Method and a device for recovery of energy from media containing combustible substances even at low concentration
EP0780633A3 (fr) * 1995-12-20 1999-01-27 H KRANTZ-TKT GmbH Dispositif pour la combustion d'impuretés dans un courant de milieu
US5823770A (en) * 1997-02-26 1998-10-20 Monsanto Company Process and apparatus for oxidizing components of a feed gas mixture in a heat regenerative reactor
WO2009059749A3 (fr) * 2007-11-07 2009-08-20 Gerd Wurster Installation de séchage
DE102008011938B3 (de) * 2008-02-29 2009-09-10 Arge Schedler - Thalhammer Vorrichtung zur Reinigung von schadstoffhaltigem Abgas
DE102009055942A1 (de) * 2009-11-26 2011-06-01 Chemisch-Thermische Prozesstechnik Gmbh Verfahren und Vorrichtung zur Reinigung von Abgasen
DE102009055942B4 (de) * 2009-11-26 2012-02-02 Chemisch-Thermische Prozesstechnik Gmbh Verfahren und Vorrichtung zur Reinigung von Abgasen
DE102009055942C5 (de) * 2009-11-26 2015-12-17 Chemisch-Thermische Prozesstechnik Gmbh Verfahren und Vorrichtung zur Reinigung von Abgasen
US9272240B2 (en) 2009-11-26 2016-03-01 Chemisch Thermische Prozesstechnik Gmbh Method and device for purifying exhaust gases

Also Published As

Publication number Publication date
EP0440181B1 (fr) 1993-09-29
EP0440181A3 (en) 1991-11-13
DE59100409D1 (de) 1993-11-04

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