METHOD OF SIMULTANEOUS REMOVAL OF NO AND CARBON PARTICLES AND INORGANIC DUST FROM FLUE GASES AND CATALYTIC REACTOR FOR REMOVAL OF NO AND CARBON PARTICLES AND INORGANIC DUST FROM FLUE GASES

Abstract

The method of simultaneous removal of NO and carbonic particles and inorganic dust from flue gases in the reactor equipped with the catalyst for direct decomposition of nitric oxide located on a metallic monolith consists in tangential introduction of flue gases to the reactor circumfer-ence generating rotational flow of the flue gases downwards of the reactor with simultaneous flow disturbance due to flue gases contact with undulating surface of metallic foil located on an inner wall of the reactor chamber and split of the flue gases by contact with the catalyst located on a spiral band falling to the lower part of the reactor, and next flue gases jet direction counter-currently to a cylindrical inner chamber containing the slices of the monolithic catalyst disturbing laminar flow of the flue gases jet. The deposited solid particles of the pollutants are collected in the lower part of the re-actor. The invention concerns also the reactor designed for simultaneous removal of NO and carbon particles and inorganic dust from flue gases.

Claims

1-28. (canceled)

29. A method comprising: a) receiving flue gasses into a reactor including a body, wherein the body includes a heated annular inner wall with an undulating inner wall surface, and wherein the received flue gases are directed to move rotationally within the body by the inner wall, b) directing the rotationally moving flue gasses downwardly within the body by engagement with a spiral band coated with a catalyst operative to directly remove NO from the gasses, c) enabling the gas that has been directed downwardly by the band to pass upwardly through a cylindrical heated chamber within the body to a flue gas outlet from the body, wherein the chamber includes a plurality of slices including the catalyst, whereby NO, carbonic particles and inorganic dust are removed from the gas by the reactor.

30. The method of claim 29, wherein in the chamber the plurality of slices extend parallel to one another and at least one directing spacer is positioned intermediate of the at least some of the plurality of slices, wherein in (c) the at least one directing spacer disturbs laminar flow of the flue gases through the chamber.

31. The method of claim 29 wherein within the chamber, a directing spacer is positioned intermediate of at least two of the plurality of slices, wherein the plurality of slices are arranged nonparallel to one another, wherein in (c) the directing spacer is operative to disturb the laminar flow of the flue gases through the plurality of slices.

32. The method of claim 29, wherein the plurality of slices have various shapes and dimensions, and wherein in (c) the gas passes through slices having various shapes and dimensions.

33. The method of claim 29, wherein in (a), the flue gases inside the reactor body are in the range of 150 C.-450 C.

34. The method of claim 29, wherein in at least one of (b) and (c), simultaneous removal of NO and total oxidation of carbonic particles contained in dust transported by the flue gasses occurs.

35. The method of claim 29, wherein in (a) the flue gasses are received in the reactor from a stationary emission source.

36. Apparatus comprising: a reactor configured for removal of NO, carbonic particles and inorganic dust from flue gases including: a reactor body configured to extend along a vertical axis wherein the reactor body includes a portion having a cylindrical shape the portion including an annular inner wall, wherein the inner wall includes an undulating inner surface, an annular outer wall, heat resistant material extending intermediate of the inner wall and the outer wall, an upper part, a closed lower end, an inner wall heater configured to heat the inner wall, a cylindrical chamber, wherein the chamber is concentric with and disposed radially inward from the inner wall, a chamber heater configured to heat the chamber, a spiral band, wherein the spiral band is disposed radially intermediate of the inner wall and the chamber, is configured to direct gas toward the lower end, is coated with a catalyst operative to directly remove NO wherein the chamber includes a chamber interior, wherein a plurality of slices including the catalyst extend in the chamber interior, wherein the slices are configured to enable axial flow of gas in the chamber interior, a flue gas inlet, wherein the flue gas inlet is configured to enable flue gas to enter the reactor body adjacent to the upper part between the inner wall and the chamber, and radially offset from the axis, a gas outlet, wherein the gas outlet is configured to enable gas to exit from the chamber interior, whereby flue gas entering the reactor from the gas inlet is caused to flow within the body with exposure to the catalyst, annularly and downwardly outside the chamber and then axially upward through the chamber interior to the gas outlet.

37. The apparatus of claim 36, wherein the chamber is bounded by a cylindrical wall, wherein the wall includes a chamber inner surface, wherein the chamber inner surface is coated with the catalyst.

38. The apparatus of claim 36, wherein within the chamber interior the slices are configured parallel to one another and perpendicular to the vertical axis.

39. The apparatus of claim 36, and further including a directing spacer, wherein the directing spacer is intermediate of at least two of the slices, whereby the directing spacer is operative to disturb laminar flow of the flue gases through the chamber interior.

40. The apparatus of claim 39, and further including a plurality of directing spacers wherein each directing spacer extends intermediate of respective immediately adjacent slices.

41. The apparatus of claim 40, wherein each directing spacer is configured to cause rotational flow of the flue gases.

42. The apparatus of claim 41, wherein each directing spacer includes a propeller shape.

43. The apparatus of claim 36, and further comprising an axial heater, wherein the axial heater extends within the chamber interior and along the vertical axis.

44. The apparatus of claim 36 wherein in the chamber includes a chamber inlet to the chamber interior, and further includes a directing spacer, wherein the directing spacer is configured to disturb laminar flow of flue gasses, wherein flue gasses are caused to flow through the directing spacer before entering the chamber inlet.

45. The apparatus of claim 36, wherein in the plurality of slices includes respective adjacent pairs of slices, wherein the slices of a respective pair extend at different angles relative to the vertical axis such that the slices of the pair are closer to each other along a direction transverse of the vertical axis.

46. The apparatus of claim 36, wherein the cylindrical chamber touches the undulating inner surface.

47. The apparatus of claim 36, wherein the reactor body includes a conical shaped portion below the portion having the cylindrical shape.

48. The apparatus of claim 36, wherein simultaneously within the reactor, NO is removed from the flue gases, carbonic particles contained in dust transported by flue gases is oxidized and inorganic dust from flue gases is removed.

Description

[0020] The examples of reactor structure according to the invention are shown on the schematic drawings.

[0021] A longitudinal-section and cross-section of the reactor are shown in FIG. 1 for the ratio L/d<50.

[0022] The longitudinal-section of the reactor for ratio L/d>50 is shown in FIG. 2.

[0023] The spiral band, which is performed in one part is shown on FIG. 3

[0024] The spiral band, which is prepared in separate parts is shown in FIG. 4.

[0025] The directing spacer is shown in FIG. 5.

[0026] The slices of the monolithic catalyst installed under the various angles are shown in FIG. 6.

[0027] The slices of the monolithic catalyst situated parallel towards each other are shown in FIG. 7.

[0028] And the slices of the monolithic catalyst with various sizes of their cross-section are shown in FIG. 8.

[0029] The example of the reactor structure according to the invention is made out for ratio of the dimensions L/d<50. The dusty gas generating in a stable emission source is supplied using feeding channel 1 which is thermally insulated from environment impact and the gas is introduced using the dusty gas inlet 2 tangentially to the surface of the cylindrical chamber with the undulating inner surface 3 for removal of NO and solid particles as well as for the oxidation of carbonic particles presented in dust transported by the gaseous jet. The catalyst enabling the removal of NO from the gaseous mixture and oxidation of carbonic particles occurs on the undulating cylindrical surface prepared using acid-proof austenitic steel foil. The oxide phases created on the acid-proof austenitic steel foil by oxidation are liable to arise as the catalyst. Inside the cylindrical and undulating chamber 3 the spiral band 4 made of the austenitic acid-proof steel covered by the oxide phases is located and it is falling downwards of the chamber 3 and it is the support of the catalyst for removal of NO and for the oxidation of carbonic particles contained in the dust. The spiral band may be prepared as one part or it may be prepared from separate parts creating the band, as it is shown on FIG. 4, but distances between the individual bond parts should not overlap according to the band pitch. The spiral band 4 is stretched out on the band frame 15. The cylindrical and undulating reactor chamber 3 is placed in the casing composed of the cylindrical part 5a and the conical part 5b. The casing contains thermal insulation, e.g. a light heat-resistant insulating material, and the insulation is placed between the two coaxial walls: the outer casing wall 6a and the inner casing wall 6b but the heater 7 of the casing is in touch with the inner casing wall 6b. The conical part 5b of the reactor in its lower part is equipped with the tight closure 8, which is simultaneously a periodically cleaned dust container. In the geometrical axis of the cylindrical undulating chamber 3 a heated chamber of.the slices of the monolith catalyst 9 is placed and its surface are covered by the active component of the catalyst. In the heated chamber of the slices of the monolith catalyst 9 the slices of the monolithic catalyst 10 and/or 16 are located and they are of different area of the channel cross-sections. The slices of the monolithic catalyst 10 and/or 16 are covered by the same active component of the catalyst as the cylindrical chamber of the reactor with undulating surface 3 and the spiral band 4.

[0030] If the ratio L/d<50 the directing spacer 11 shown on FIG. 5, is not situated in the front of the inlet to porous support of the catalyst 10 and/or 16. The directing spacer 11 consists of the blades 17, which are sloped at small angle towards level and fastened between the outer ring 18 and the inner ring 19. On the wall of heated chamber of the slices of the monolithic catalyst 9 the chamber heater 12 is installed. In the geometrical axis of the heated chamber of the slices of the monolithic catalyst 9 an additional axial heater 13 is located. The heated chamber of the slices of the monolithic catalyst 9 is equipped with the gaseous outlet 14. The slices of the monolithic catalyst 10 may be placed under the various angles (alpha) or (beta) towards the axis of the heated chamber of the slices of the monolith catalyst 9 as it is shown in FIG. 6, in order to attain a change of the flow direction for achieving an effect of inlet flow to the slice of the monolith catalyst. At the time the directing spacers 11 are not applied. The channels 20 in slice of the monolithic catalyst are shown in FIG. 6. The change of the flow direction before the inlet to the slices of the monolithic catalyst is achieved when the slices of the monolithic reactor are parallel towards themselves, but under angle (alpha) towards the axis of the heated chamber of the monolithic slices of the catalyst 9, as it is shown in FIG. 7. There is a space filled by the flue gases jets between the slices of the monolithic catalyst 10 with both arrangement of the slices of the monolith catalyst 10 shown in FIGS. 6 and 7.

[0031] The example of the structure of the reactor according to the invention shown in FIG. 2 is designed for the case of the dimensions ratio L/d>50. The difference in the example of the structure shown in FIG. 2 in comparison with the structure shown in FIG. 1 is in the location of the directing spacer 11 in the front of the inlet to the porous slice of the monolithic catalyst 10 or 11, when the front of the porous support of the catalyst 10 is in position that the ratio L/d>50.

[0032] In both the cases of the realization the length of the heated chamber of the slices of the monolithic catalyst 9 should be as long as possible in order to achieve maximum distance for the flow of the flue gases.

It is possible to apply the slices of the monolithic catalyst 16 with the area cross-sections of the channels different from the area cross-sections of the channels of the slices of the monolithic catalyst 10, that is seen in FIG. 8.

[0033] The slices of the monolithic catalyst 10 are of the same or the various shapes and dimensions of the channels cross-sections and each chamber may contain the slices of the monolithic catalyst with the various shapes and cross-sections.