WO2003000400A1 - Catalyst or sorbent beds - Google Patents
Catalyst or sorbent beds Download PDFInfo
- Publication number
- WO2003000400A1 WO2003000400A1 PCT/GB2002/002520 GB0202520W WO03000400A1 WO 2003000400 A1 WO2003000400 A1 WO 2003000400A1 GB 0202520 W GB0202520 W GB 0202520W WO 03000400 A1 WO03000400 A1 WO 03000400A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- bed
- deflector
- catalyst
- fixed
- sorbent
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C3/00—Cyanogen; Compounds thereof
- C01C3/02—Preparation, separation or purification of hydrogen cyanide
- C01C3/0208—Preparation in gaseous phase
- C01C3/0212—Preparation in gaseous phase from hydrocarbons and ammonia in the presence of oxygen, e.g. the Andrussow-process
- C01C3/022—Apparatus therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
- B01J8/025—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical shaped bed
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0292—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds with stationary packing material in the bed, e.g. bricks, wire rings, baffles
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/20—Nitrogen oxides; Oxyacids of nitrogen; Salts thereof
- C01B21/24—Nitric oxide (NO)
- C01B21/26—Preparation by catalytic or non-catalytic oxidation of ammonia
- C01B21/267—Means for preventing deterioration or loss of catalyst or for recovering lost catalyst
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/20—Nitrogen oxides; Oxyacids of nitrogen; Salts thereof
- C01B21/24—Nitric oxide (NO)
- C01B21/26—Preparation by catalytic or non-catalytic oxidation of ammonia
- C01B21/28—Apparatus
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/386—Catalytic partial combustion
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
- C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
- C07C45/37—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups
- C07C45/38—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups being a primary hydroxyl group
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/30—Physical properties of adsorbents
- B01D2253/34—Specific shapes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/204—Inorganic halogen compounds
- B01D2257/2045—Hydrochloric acid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/93—Toxic compounds not provided for in groups B01D2257/00 - B01D2257/708
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/261—Drying gases or vapours by adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00823—Mixing elements
- B01J2208/00831—Stationary elements
- B01J2208/0084—Stationary elements inside the bed, e.g. baffles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00884—Means for supporting the bed of particles, e.g. grids, bars, perforated plates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
- C01B2203/0261—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a catalytic partial oxidation step [CPO]
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1005—Arrangement or shape of catalyst
Definitions
- This invention relates to fixed beds of catalyst or sorbent and in particular, in order to increase the effectiveness of the bed, to means for directing the flow of a gas or liquid passing through the bed away from regions of the bed having a higher permeability.
- Fixed catalyst and sorbent beds generally comprise at least one layer of a catalyst or sorbent with optionally an inert material, in the form of particles such as extrudates, pellets or granules supported by a perforate member such as a perforate plate, grid or mesh.
- sorbent we necessarily include both adsorbent and absorbent materials.
- a gas or liquid must flow through the interstices or voids between the particles and the opposition to the flow causes a pressure drop to occur between one side of the bed and the other.
- the pressure drop across the bed should be as low as possible and hence the permeability of the bed should be high whilst at the same time providing sufficient contact time between the particles and gas or liquid to efficiently perform the catalysis or sorption processes.
- the flow of gas or liquid through the bed of catalyst or sorbent is uniform to provide consistent operation in terms of conversion in the case of a catalyst bed, or absorption in the case of an absorbent bed.
- the size of the particles and thickness of the layer of particles is carefully controlled to achieve a uniform particle shape and size and a uniform permeability through the bed, through which the gas or liquid may flow.
- a problem encountered with fixed beds containing particles of catalyst or sorbent is that where the particles make contact with the means for containing the bed and/or any member transecting the bed that is aligned with the flow of fluid through the bed, it has been found that the permeability is greater and hence the flow of gas or liquid through the bed is higher.
- the present invention provides a fixed bed containing particles of a catalyst or sorbent through which a process fluid is to pass wherein the bed is bounded by process fluid-impermeable boundary means having a process fluid-impermeable deflector extending away from said boundary and contacting said bed, whereby part of said particulate catalyst or sorbent is disposed between the position where said deflector means contacts the bed and said boundary means from which said deflector means extends.
- the fixed beds may be subjected to axial and / or radial flow of the process fluid which may be gaseous or liquid.
- the beds of the present invention are subject to axial flow and may be disposed, for example, substantially horizontally in the vessel with gas and/or liquid passing substantially vertically through the bed.
- the beds generally comprise particles of catalyst or sorbent supported by a perforate member such as perforate plates, meshes or grids having appropriately-sized holes to prevent passage of the particles therethrough.
- the bed is typically bounded by the vessel wall or an edge member that extends from the perforate plate for at least the depth of the bed, and which may be attached to the perforate plate, vessel wall or other supporting means for the bed.
- Such edge members are generally impermeable to process fluid. Where the bed is subjected to elevated temperatures, such edge members may be described as heat-shields as they prevent contact of the hot catalyst particles with e.g. the bed support means or vessel wall.
- the beds may be of any shape necessary to provide the required task. Often the bed shape matches that of the cross-section of the vessel in which it is disposed. For example, the bed may be circular, oval, square, rectangular, hexagonal or octagonal.
- the cross-section width may vary in the range of 0.25 m to 6 m and is preferably 0.5 m to 3.5 m.
- the present invention is of particular utility where the beds are relatively thin, i.e. having a depth less than the vessel diameter.
- the beds of the present invention are thin beds, typically with a depth between 5 and 500 mm, more preferably between 25 and 300 mm, and most preferably between 25 and 100 mm.
- the particles of catalyst or sorbent are in the form of spheres, platelets, cubes, extrudates, cylindrical pellets, granules or other regular or irregular shapes, generally having an aspect ratio, i.e. the largest dimension divided by the smallest dimension, of less than 2.
- the size of the particles may be uniform or different as required to create the desired contact time between gas or liquid and catalyst or sorbent.
- the deflector means of the present invention may be any that results in the deflection of process fluid.
- such deflector means may comprise a plate, impermeable to process fluid, extending from the boundary means and into or onto the bed.
- the thickness of the deflector plate will depend upon a number of factors including the dimensions of the vessel and/or bed but is preferably in the range of 1-25 mm, more preferably 1-10 mm and most preferably 2-5 mm.
- the deflector plate may be continuous or discontinuous around the boundary means.
- the deflector plate may be shaped, in particular to deflect the process fluid into or onto the bed of catalyst or sorbent at angles preferably in the range of about 1 - 90 degrees and more preferably 1 - 60 degrees from the direction of flow of the process fluid through the bulk of the bed.
- the deflector plate so disposed will cover an area of the bed between the boundary means and the position where the deflector contacts the bed. This area may be expressed as a percentage of the total surface area of the bed.
- the area is between 0.1 and 40%, preferably between 0.1 and 15% and most preferably between 0.3 and 10% in total of the surface area of the bed.
- the deflector extends beneath the surface of the bed, preferably for a distance equal to between 5 and 90% of the thickness of the bed.
- the deflector contacts the surface of the bed. It is desirable that the contact with the surface of the bed is maintained through a number of heat-cool cycles. This may be achieved for example by means of a flexible deflector plate or plates, attached to the boundary means by hinging means.
- the deflector may be fabricated from any material suitable for use under the conditions of the catalytic or sorbent processes.
- the deflector is fabricated from stainless steel, for example 310 stainless steel.
- the deflector in a circular bed the deflector is disposed preferably in at least part of the circumferential region, or in a rectangular bed the deflector may be along at least part of the outer edge. If columns, pillars or other members transect the bed, it may also be desirable to provide a deflector plate around such members.
- the deflector may be provided for a fixed bed containing particles of a catalyst.
- the catalyst may be any that is used disposed in thin beds.
- Processes that may utilise catalysts in thin beds include for example, ammonia oxidation using, e.g. a particulate cobalt-based catalyst, hydrodesulphurisation using e.g. a cobalt- or nickel-molybdate hydrodesulphurisation catalyst, hydrogen cyanide manufacture, formaldehyde manufacture and partial oxidation reactions, for example for the partial oxidation of hydrocarbons as part of so- called 'gas-to-liquid' (GTL) processes.
- GTL gas-to-liquid'
- the deflector may also be provided for a fixed bed containing particles of a sorbent material.
- a sorbent material suitable for the removal of sulphur, mercury, arsenic or compounds thereof, water and/or hydrogen chloride from process fluids, e.g. hydrocarbons, may be used.
- sorbents include basic zinc carbonate and copper / zinc oxides for sulphur removal, copper sulphide for mercury and arsenic removal and sodium aluminate or lead carbonate for hydrogen chloride removal.
- the present invention is of utility where the bed is subjected to elevated temperatures.
- the bed temperatures are preferably greater than 100°C, more preferably greater than 200°C, and most preferably greater than 500°C.
- Figures 1 is diagrammatic cross section of an edge region of a circular fixed catalyst or sorbent bed in accordance with a first example, wherein the deflector is a continuous circumferential plate attached to the vessel wall, the deflector extending from said vessel wall
- Figure 2 is a diagrammatic cross section of an edge region of a fixed catalyst bed in accordance with a second example wherein the deflector comprises a continuous circumferential plate attached to a heat shield fixed to the bed support, and
- Figure 3 is a diagrammatic cross section of an edge region of a fixed catalyst bed in accordance with a third example, wherein the deflector comprises a series of plates attached to a heat shield by hinging means
- Figure 1 shows a bed of a catalyst or sorbent particles 10 supported upon a perforate member 11 having orifices 12 present to allow the flow of gas or liquid through the bed and contained by an edge member 13
- the perforate member is held in position by a lug 14 present on the vessel wall 15
- a deflector plate 16 is attached to the vessel wall above the surface of the bed The deflector plate 16 extends from the vessel wall 15 over the surface of the bed, enters the bed at a position 17, away from the edge region, and extends to a depth approximately 50% of the thickness of the bed at an angle of approximately 15 degrees to the angle of fluid flow through the bulk of the bed
- a catalyst bed for the oxidation of ammonia is provided by a layer of cobalt- containing catalyst particles 20 supported on a perforate member 21 having orifices 22 to allow the flow of gases through the bed
- the perforate member is supported by a lug 23 attached to a bed-support 24
- the particles 20 are contained at the edge of the bed by means of a heat- shield 25 attached to bed support 24 that prevents contact of the catalyst particles with said bed support
- a deflector plate 26 is attached to the heat shield at a position above the surface of the bed The deflector plate 26 extends from the heat-shield 25 over the surface of the bed, enters the bed at a position 27, away from the edge region, and extends to a depth approximately 50% of the thickness of the bed at an angle of approximately 10 degrees to the angle of fluid flow through the bulk of the bed
- a catalyst bed for the oxidation of ammonia is provided by a layer of cobalt- containing catalyst particles 30 supported on a perforate member 31 having orifices 32 to allow the flow of gases through the bed
- the perforate member is supported by a lug 33 attached to a bed support 34
- the particles 30 are contained at the edge of the bed by means of a heat- shield 35, attached to the bed support 34, that prevents contact of the catalyst particles with said bed support
- a deflector plate 36 is attached to the heat shield at a position above the surface of the bed by hinging means 37
- the deflector plate 36 extends from said heat shield and contacts with the particles of the bed at a position 38, away from the edge region at an angle of approximately 80 degrees to the angle of fluid flow through the bulk of the bed
- a catalyst bed of a cobalt-rare earth perovskite for the oxidation of ammonia as described in WO98/28073, disposed in a reactor of 0.5 - 6 m circular cross-section has a continuous circumferential deflector plate of width 1-20 cm extending from the heat shield and into the bed to a depth between 2-20 mm at an angle of approximately 10-45 degrees to the angle of fluid flow through the bulk of the bed.
- the catalyst particles are typically cylindrical pellets of 3 mm length and 3 mm diameter and are present in the bed at a depth of 25 - 150 mm. They are supported on a layer of ⁇ -alumina pellets of typically 3 - 10 mm diameter of depth 25 - 150 mm.
- the deflector reduces the amount of unreacted ammonia in the product gas stream.
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB0115296.6 | 2001-06-22 | ||
GB0115296A GB0115296D0 (en) | 2001-06-22 | 2001-06-22 | Catalyst or sorbent beds |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2003000400A1 true WO2003000400A1 (en) | 2003-01-03 |
Family
ID=9917158
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/GB2002/002520 WO2003000400A1 (en) | 2001-06-22 | 2002-05-30 | Catalyst or sorbent beds |
Country Status (2)
Country | Link |
---|---|
GB (1) | GB0115296D0 (en) |
WO (1) | WO2003000400A1 (en) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7563419B2 (en) * | 2002-07-03 | 2009-07-21 | Yara International Asa | Method and device for supporting catalyst gauzes in an ammonia oxidation burner |
WO2013034303A1 (en) * | 2011-09-09 | 2013-03-14 | Thyssenkrupp Uhde Gmbh | Apparatus for minimizing bypass in ammonia oxidation burners of industrial plants with burner diameters of 2-7 m in natural- or forced-circulation boilers |
WO2013034304A1 (en) * | 2011-09-09 | 2013-03-14 | Thyssenkrupp Uhde Gmbh | Apparatus for minimizing bypass in ammonia oxidation burners |
Citations (4)
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---|---|---|---|---|
DE1086215B (en) * | 1959-02-13 | 1960-08-04 | Pintsch Bamag Ag | Device for distributing the sprinkling fluid in columns filled with fillers for absorption, distillation purposes and the like. like |
EP0293523A1 (en) * | 1987-06-01 | 1988-12-07 | Uop Inc. | Mixing device for vertical flow fluid-solid contacting |
US5514205A (en) * | 1994-12-30 | 1996-05-07 | Awaji; Toshio | Apparatus for removing harmful objects from a gas |
US5882385A (en) * | 1995-12-05 | 1999-03-16 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Plant for treating at least one fluid and use for the separation of at least one constituent of a gas mixture |
-
2001
- 2001-06-22 GB GB0115296A patent/GB0115296D0/en not_active Ceased
-
2002
- 2002-05-30 WO PCT/GB2002/002520 patent/WO2003000400A1/en not_active Application Discontinuation
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE1086215B (en) * | 1959-02-13 | 1960-08-04 | Pintsch Bamag Ag | Device for distributing the sprinkling fluid in columns filled with fillers for absorption, distillation purposes and the like. like |
EP0293523A1 (en) * | 1987-06-01 | 1988-12-07 | Uop Inc. | Mixing device for vertical flow fluid-solid contacting |
US5514205A (en) * | 1994-12-30 | 1996-05-07 | Awaji; Toshio | Apparatus for removing harmful objects from a gas |
US5882385A (en) * | 1995-12-05 | 1999-03-16 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Plant for treating at least one fluid and use for the separation of at least one constituent of a gas mixture |
Cited By (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7563419B2 (en) * | 2002-07-03 | 2009-07-21 | Yara International Asa | Method and device for supporting catalyst gauzes in an ammonia oxidation burner |
WO2013034303A1 (en) * | 2011-09-09 | 2013-03-14 | Thyssenkrupp Uhde Gmbh | Apparatus for minimizing bypass in ammonia oxidation burners of industrial plants with burner diameters of 2-7 m in natural- or forced-circulation boilers |
DE102011112782A1 (en) * | 2011-09-09 | 2013-03-14 | Thyssenkrupp Uhde Gmbh | Device for bypass reduction in ammonia oxidation burners |
WO2013034304A1 (en) * | 2011-09-09 | 2013-03-14 | Thyssenkrupp Uhde Gmbh | Apparatus for minimizing bypass in ammonia oxidation burners |
CN103857621A (en) * | 2011-09-09 | 2014-06-11 | 蒂森克虏伯工业解决方案有限公司 | Apparatus for minimizing bypass in ammonia oxidation burners of industrial plants with burner diameters of 2-7m in natural- or forced-circulation boilers |
AU2012306722B2 (en) * | 2011-09-09 | 2015-10-29 | Thyssenkrupp Uhde Gmbh | Apparatus for minimizing bypass in ammonia oxidation burners of industrial plants with burner diameters of 2-7 m in natural- or forced-circulation boilers |
AU2012306723B2 (en) * | 2011-09-09 | 2016-01-21 | Thyssenkrupp Industrial Solutions Gmbh | Apparatus for minimizing bypass in ammonia oxidation burners |
US9242216B2 (en) | 2011-09-09 | 2016-01-26 | Thyssenkrupp Industrial Solutions Ag | Apparatus for minimizing bypass in ammonia oxidation burners of industrial plants with burner diameters of 2-7 M in natural- or forced-circulation boilers |
EP2753576B1 (en) | 2011-09-09 | 2016-02-03 | ThyssenKrupp Industrial Solutions AG | Apparatus for minimizing bypass in ammonia oxidation burners |
US9383099B2 (en) | 2011-09-09 | 2016-07-05 | Thyssenkrupp Industrial Solutions Gmbh | Apparatus for minimizing bypass in ammonia oxidation burners |
EA026351B1 (en) * | 2011-09-09 | 2017-03-31 | Тюссенкрупп Индастриал Солюшнс Гмбх | Apparatus for minimizing bypass in ammonia oxidation burners of industrial plants with burner diameters of 2-7 m in natural- or forced-circulation boilers |
EA026206B1 (en) * | 2011-09-09 | 2017-03-31 | Тюссенкрупп Индастриал Солюшнс Гмбх | Apparatus for minimizing bypass in ammonia oxidation burners |
Also Published As
Publication number | Publication date |
---|---|
GB0115296D0 (en) | 2001-08-15 |
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