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WO1999025650A1 - Catalyseurs d'oxydation de l'ammoniac - Google Patents

Catalyseurs d'oxydation de l'ammoniac Download PDF

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Publication number
WO1999025650A1
WO1999025650A1 PCT/GB1998/003386 GB9803386W WO9925650A1 WO 1999025650 A1 WO1999025650 A1 WO 1999025650A1 GB 9803386 W GB9803386 W GB 9803386W WO 9925650 A1 WO9925650 A1 WO 9925650A1
Authority
WO
WIPO (PCT)
Prior art keywords
meshes
unit according
particles
catalyst
cartridge
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/GB1998/003386
Other languages
English (en)
Inventor
Bernard John Crewdson
Andrew Mark Ward
Michael David Dunne
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Imperial Chemical Industries Ltd
Original Assignee
Imperial Chemical Industries Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Imperial Chemical Industries Ltd filed Critical Imperial Chemical Industries Ltd
Priority to AU10460/99A priority Critical patent/AU733971B2/en
Priority to EP98952918A priority patent/EP1034134A1/fr
Priority to CA002306780A priority patent/CA2306780A1/fr
Publication of WO1999025650A1 publication Critical patent/WO1999025650A1/fr
Priority to NO20002522A priority patent/NO20002522D0/no
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/248—Reactors comprising multiple separated flow channels
    • B01J19/2495—Net-type reactors
    • 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
    • B01J8/0207—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 horizontal
    • B01J8/0214—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 horizontal in a cylindrical annular shaped bed
    • 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
    • C01B21/265—Preparation by catalytic or non-catalytic oxidation of ammonia characterised by the 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
    • 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

Definitions

  • This invention relates to ammonia oxidation catalysts
  • Ammonia oxidation is widely employed in the manufacture of nitric acid and hydrogen cyanide
  • ammonia is oxidised with air to nitric oxide
  • hydrogen cyanide a mixture of ammonia and methane (often as natural gas) is oxidised with air
  • the gas mixture is passed at an elevated temperature over a catalyst to effect the oxidation
  • Side reactions such as the formation of nitrogen or nitrous oxide, are undesirable Consequently, in addition to good activity, the catalyst is required to have a good selectivity
  • the catalysts employed have been platinum, sometimes alloyed with other precious metals, in the form of meshes or gauzes formed from the metal wire
  • Such catalysts have good activity and selectivity but suffer from the disadvantage that not only is the catalyst very expensive, but at the temperatures encountered, the metals exhibit an appreciable volatility and so gradually the metal is lost into the gas stream
  • it is well known to provide downstream means to trap the volatilised metal so that it may be recovered subsequently, because of the continual volatilisation, the life of the catalyst is short and frequent replacement is necessary
  • the recovery of the metals from the downstream trap and re-fabrication of the catalyst meshes or gauzes involves a considerable allocation of working capital
  • Ammonia oxidation is normally operated by passing the heated ammonia/air mixture at a high linear velocity (measured at NTP) through a wad of precious metal meshes or gauzes extending across the cross-section of the reactor
  • Commercial ammonia oxidation plants usually employ reactors having a diameter in the range 0 5 to 5 m
  • Linear gas velocities conventionally employed in commercial ammonia oxidation processes operating substantially at atmospheric pressure are usually in an excess of 2000 m/h, and typically are in the range 5000-10000 m/h, preferably 4000-6000 m/h
  • e g up to 10 barg Jhe linear velocities are generally in the range 20000 to 50000 m/h
  • the catalyst should be in a form such that it is a direct replacement for the precious metal meshes or gauzes conventionally used.
  • the temperature to which the feed gas must be pre-heated in order that the oxidation process may sustain itself is termed the "blow out” temperature.
  • the "blow-out” temperature is below 250°C, particularly below 150°C.
  • the bed depth should be as great as possible and the particle size as small as possible.
  • the pressure drop experienced by the gas as it passes through the catalyst bed This increases as the particle size of the catalyst is decreased and as the catalyst bed depth increases, and so a compromise is necessary to achieve an acceptable "blow-out" temperature while at the same time have an acceptable pressure drop.
  • the bed depth should be less than 50 mm.
  • the space velocity is 10 5 h '1 .
  • space velocities above 10 5 hJ are normally required.
  • the catalyst bed in the form of a cartridge that can replace the conventional wad of meshes or gauzes.
  • an ammonia oxidation catalyst bed cartridge unit comprising a pair of retaining meshes spaced apart by less than 50 mm defining an enclosure filled with a random packed mass of particles of a composition comprising oxides of at least one metal selected from manganese, iron, nickel and cobalt , said particles having a minimum dimension of at least 0 5 mm and a maximum dimension of not more than 5 mm, the spacing between said meshes being at least 4 times, and less than 50 times, the maximum dimension of the particles
  • the cartridge may comprise three spaced gauzes with the smaller particles between the middle, or intermediate, gauze and the lower gauze and the larger particles between the upper and intermediate gauzes
  • the intermediate gauze is disregarded in determining the spacing of the gauzes
  • the meshes which may be of a suitable heat resistant metal such as stainless steel, should have as large an aperture as is consistent with retaining the particles on the mesh
  • the meshes are preferably catalytically inert
  • the cartridge unit may comprise a pair of spaced apart mesh sheets dimensioned so as to fit across the reactor
  • the mesh sheets may be held spaced apart by a suitable spacing member disposed round the periphery of the unit Spacing members may also be disposed at intervals across the unit
  • the unit is preferably dimensioned such that it is a snug fit inside the ammonia oxidation reactor and extends across the cross-section of the reactor
  • the cartridge may comprise a supporting unit, for example a grid or apertured plate dimensioned so as to fit across the reactor with a cartridge sub-unit positioned in each aperture of the plate or grid, with each sub-unit comprising a pair of spaced apart meshes with the catalyst disposed between the meshes
  • the catalyst particles may be irregular granules or may be moulded or formed into geometric shapes, such as cylinders
  • Preferred catalyst particles are moulded cylindrical tablets having a diameter in the range 0 5 to 4 mm and a length of 0 5 to 4 mm
  • the aspect ratio of the particles, i e the ratio of the maximum dimension to the minimum dimension is preferably less than 2 Moulded particles, e g cylinders, may have one or more passages therethrough to increase the geometric surface area and to increase the bed voidage thereby reducing the pressure drop across the bed
  • the bed depth, i e the spacing between the meshes is preferably 5 to 20 times the maximum dimension of the shaped particles
  • the catalyst may be in a form wherein the amount of oxygen is non-stoichiomet ⁇ c This arises from the variable valency of cobalt and also of any variable valency rare earth present as part, or all, of element A
  • the catalyst particles may be made by forming a finely divided powder composition into particles of the desired size by techniques such as granulation, extrusion or moulding
  • the finely divided powder composition may be made by precipitation by adding a solution of soluble salts of the relevant metals to a solution of a base, e.g. ammonium carbonate or hydroxide, to precipitate the relevant metals as (basic) carbonates, hydroxides, or oxides followed by calcination to convert the precipitated compounds to the oxides
  • a base e.g. ammonium carbonate or hydroxide
  • the precipitation may alternatively, but less preferably, be effected by adding the base to the solution of the mixed salts.
  • the active metal is cobalt
  • the finely divided powder composition may be made by forming a solution of thermally decomposable salts, e.g.
  • the composition may be made by mixing preformed oxides of the metals in the appropriate proportions
  • the active material e.g. cobalt may be present as a coating on suitable support particles.
  • a finely divided oxidic material e.g.
  • ce ⁇ a may be impregnated with a solution containing a cobalt salt, and possibly also salts of other elements such as a salt of an element A, e.g a lanthanum salt, followed by decomposition of the salts.
  • a supported material may be made by precipitation by precipitating the cobalt, and optionally other elements, as heat decomposable compounds on to a finely divided, e.g precipitated, oxidic support compound or compound decomposable thereto
  • the composition should be calcined, e g in air, preferably at a temperature in the range 900-1200°C, before or preferably after granulating, extruding or moulding into particles of the desired size and shape
  • Figure 2 is a diagrammatic cross section of a part of unit in accordance with a second embodiment of the invention
  • Figure 3 is a diagrammatic cross section through an ammonia oxidation reactor incorporating a unit of the present invention
  • Figure 4 is a plan view of part of a wire gauze showing cuts and fold lines
  • Figure 5 is a sketch of part of a gauze as shown in Figure 4 folded to form a compartmentalised structure.
  • Figure 6 is a diagrammatic cross section of a unit in accordance with a third embodiment of the invention
  • Figure 7 is an enlargement of part of Figure 6 showing the configuration of the cartridge sub-units of Figure 6.
  • Figure 8 is a cross section of a reactor showing the support grid and cartridge configuration of a fourth embodiment of the invention
  • FIG 9 is a sketch of one of the cartridge units of Figure 8
  • Figure 10 is a section through the cartridge unit of Figure 9.
  • a catalyst cartridge consisting of a pair of circular stainless steel meshes 1 , 2 of diameter about 3 m having a mesh size of for example about 2 mm held spaced 20 mm apart by a spacer ring 3. Additional spacer members 4 are disposed at intervals across the cartridge. The space enclosed by the meshes and the ring is filled with random packed cylindrical catalyst tablets of 3 mm diameter and 3 mm height.
  • the gauzes particularly the lower gauze, may stretch and/or sag after exposure to the prevailing operating conditions for an extended period of time.
  • the catalyst particles may re-distribute themselves so that some areas of the bed have a lesser bed depth than others. This is undesirable as the process gas will preferentially pass through the portions of lesser bed depth and insufficient reaction may occur.
  • the lower gauze is supported by a rigid porous structure such as tiles of a ceramic foam material.
  • the upper mesh may be held firmly against the bed of catalyst particles.
  • rivets 5 may be provided extending through the meshes 1 , 2 and the catalyst bed, and a spring 6 provided above the upper mesh 1 engaging with the upper mesh 1 and a cap 7 on the upper end of the rivet.
  • the spring is preferably located on the upstream side of the catalyst bed, since the temperature in operation is lower than that on the downstream side of the catalyst bed.
  • the rivets 5 may be provided in addition to, or instead of, the intermediate spacers 4 of the embodiment of Figure 1.
  • Figure 3 there is shown an ammonia oxidation reactor 10 having an inlet port 11 and an outlet port 12. Disposed across the reactor is a catalyst cartridge 13, of the type shown in Figure 1 supported by ceramic foam tiles 14 resting on cross members 15 extending across the reactor 10.
  • the lower gauze may be cut and folded to form upstanding dividing walls, preferably of height substantially equal to the desired bed depth.
  • a sheet of wire gauze 16 is cut along the lines 17, 18, 19 and 20 and then folded in alternate directions along the dotted lines a-a, b-b and c-c, and along lines d-d, e-e and f-f and d'-d', e'-e' and f-f etc. to form upstanding walls 21 , 22, 23 and 24.
  • the flaps e.g. 25 formed by the cuts 17 to 20 are then tack welded to the upstanding walls.
  • the compartments are then filled with the particulate catalyst.
  • the compartments may be of any convenient shape, e.g. square, rectangular, triangular etc.
  • a catalyst bed having different size particles may be provided by providing the cartridge with three spaced gauzes with the smaller particles between the middle gauze and the lower gauze and the larger particles between the upper and middle gauzes.
  • the lower gauze may be shaped to give compartments as shown in Figures 4 and 5 while the upper portion of the bed, i.e. containing the larger particles, is a continuous bed.
  • FIGs 6 and 7 there is shown an alternative construction for the cartridge.
  • This construction is particularly suited to embodiments where the catalyst particle size is relatively small, typically maximum dimension below 2 mm, and the bed depth shallow, e.g. less than 25 mm.
  • the cartridge consists of a circular plate 26 dimensioned to fit across the reactor, e.g. in place of cartridge 13 of Figure 3.
  • the plate has a plurality of circular apertures, e.g. of 100 mm diameter, spaced apart at e.g. 200 mm centres. Located within each aperture is a cartridge sub-unit 27.
  • Each sub-unit consists of a plate 28 having a central aperture 29 and a pair of concentric cylindrical meshes 30, 31 , typically of length 200-300 mm, fastened at one end to the plate 28. The other end of the meshes is fastened to a closure plate 32.
  • the spacing between the concentric meshes is typically 10-20 mm and the catalyst particles are disposed in the space between the two meshes 30, 31.
  • a square grid of cartridge supports 33 is disposed across the reactor and a catalyst cartridge 34 is disposed in each square of the grid.
  • the grid, and hence the cartridges need not be square, but may be of another polygonal shape, e.g. rectangular or triangular, in plan.
  • the spaces 35 in the grid at the edges of the reactor that are not large enough to receive a cartridge 34 are closed with blanking members. Alternatively cartridges of a non-standard size may be fitted in these spaces.
  • Each cartridge 34 is in the form of an inverted pyramid structure having a flange 36 by which the cartridge may be supported on the grid cartridge supports 33.
  • the pyramid consists of an outer hollow square base 37 from which angle members 38 defining the outer inclined edges of the pyramid are disposed. Triangular ceramic foam tiles 39, forming the inclined faces of the pyramid, are supported by the angle members 38. These foam tiles 39 serve to support a lower, inverted pyramidal-shaped, mesh or gauze 40 attached at its upper, base, end to the outer square base 37.
  • Supported within the outer hollow square base 37 by means of support brackets 41 spaced at intervals around the outer base 37 is a hollow inner square base 42 from which depends a second, inner, inverted pyramidal-shaped, mesh or gauze 43.
  • a spacer member 44 is disposed at the apex of the pyramid to hold the two gauzes apart.
  • the catalyst particles are disposed in the space 45 between the two gauzes.
  • the space 46 between the walls of the outer and inner square bases 37 and 42 provides a reservoir for catalyst particles so that the space 45 between the gauzes 40, 43 may be kept full of catalyst particles in the event of settlement of the catalyst particles during use. It is seen that in use, the process gas flows down through the inner hollow base 42, through inner gauze 43, through the catalyst-filled space 45, and then through outer gauze 40 and the ceramic foam tile 39 as shown by the arrows.
  • This form of cartridge construction facilitates replacement of the cartridges in the reactor and charging and discharging catalyst from the individual cartridges. It also has the benefit that optimum use may be made of the reactor cross sectional area while providing for a catalyst bed area substantially greater than that of the reactor cross sectional area.
  • the catalyst units or cartridges of the invention may be used as a direct replacement for the conventional precious metal catalysts with essentially no modification to the ammonia oxidation process, except of course the conventional precious metal trap arrangements can be eliminated.
  • the oxidation process may be operated at temperatures of 800-1000°C, particularly 850-950°C, pressures of 1 to 15 bar abs., with ammonia in air concentrations of 5-15%, often about 10%, by volume.
  • Example 1 A finely divided lanthana/ceria/cobalt oxide catalyst (La:Ce:Co atomic proportions 8:2:10) was made by precipitation followed by calcination at 900°C. The resultant powder was formed into cylindrical pellets of 3 mm diameter and 3 mm height. A preheated mixture of air and ammonia containing about 10% by volume of ammonia was passed at atmospheric pressure through a bed of 40 mm depth of the pellets at various linear velocities. The preheat temperature was gradually decreased and the temperature (“blow-out" temperature) noted at which the reaction no longer was self-sustaining. While the reaction was self-sustaining the temperature of the gas mixture leaving the catalyst bed was typically about 600-650°C higher than the preheat temperature. The procedure was repeated with a catalyst bed of 20 mm depth. The results are shown in the following table.
  • Example 1 The procedure of Example 1 was repeated but with the catalyst in the form of granules of diameter 0.5 mm and 2 mm, and cylindrical pellets as used in Example 1. In this example beds of various depths were used at a constant linear gas flow rate of 4500 m/h. The results are shown in the following table.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Inorganic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Catalysts (AREA)

Abstract

Une unité à cartouche de catalyseur d'oxydation de l'ammoniac comporte une paire de toiles de retenue espacées l'une de l'autre de plus de 50 mm, définissant une enceinte remplie d'une masse tassée de manière aléatoire constituée de particules formées d'une composition comprenant des oxydes d'au moins un métal choisi parmi manganèse, fer, nickel et cobalt, en particulier cobalt, et au moins un élément A choisi parmi les terres rares et yttrium, dans des proportions dans lesquelles le rapport entre l'élément A et le cobalt est de l'ordre de 0,8 à 1,2. Les particules du catalyseur ont une dimension minimum d'au moins 0,5 mm et une dimension maximum d'au plus 5 mm, l'espacement entre les toiles étant d'au moins 4 fois, mais pas plus de 50 fois, la dimension maximum des particules. L'unité peut s'étendre sur la section transversale du réacteur d'oxydation ou une cartouche de catalyseur peut comporter une plaque à grille ou à ouvertures, s'étendant sur la section transversale du réacteur, une unité étant prévue dans chaque ouverture.
PCT/GB1998/003386 1997-11-19 1998-11-06 Catalyseurs d'oxydation de l'ammoniac Ceased WO1999025650A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
AU10460/99A AU733971B2 (en) 1997-11-19 1998-11-06 Ammonia oxidation catalysts
EP98952918A EP1034134A1 (fr) 1997-11-19 1998-11-06 Catalyseurs d'oxydation de l'ammoniac
CA002306780A CA2306780A1 (fr) 1997-11-19 1998-11-06 Catalyseurs d'oxydation de l'ammoniac
NO20002522A NO20002522D0 (no) 1997-11-19 2000-05-16 Katalysatorer for ammoniakkoksidasjon

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB9724310.9 1997-11-19
GBGB9724310.9A GB9724310D0 (en) 1997-11-19 1997-11-19 Ammonia oxidation catalysts

Publications (1)

Publication Number Publication Date
WO1999025650A1 true WO1999025650A1 (fr) 1999-05-27

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PCT/GB1998/003386 Ceased WO1999025650A1 (fr) 1997-11-19 1998-11-06 Catalyseurs d'oxydation de l'ammoniac

Country Status (7)

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EP (1) EP1034134A1 (fr)
AU (1) AU733971B2 (fr)
CA (1) CA2306780A1 (fr)
GB (1) GB9724310D0 (fr)
NO (1) NO20002522D0 (fr)
WO (1) WO1999025650A1 (fr)
ZA (1) ZA9810270B (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102007026712A1 (de) 2007-06-06 2008-12-11 Uhde Gmbh Vorrichtung und Verfahren für katalytische Gasphasenreaktionen sowie deren Verwendung
WO2010046675A1 (fr) * 2008-10-20 2010-04-29 Johnson Matthey Plc Unité de confinement d’un catalyseur
DE102008059930A1 (de) 2008-12-02 2010-06-10 Uhde Gmbh Vorrichtung und Verfahren für katalytische Gasphasenreaktionen sowie deren Verwendung
EP2202201A1 (fr) 2008-12-23 2010-06-30 SÜD-CHEMIE CATALYSTS ITALIA S.r.l. Catalyseurs d'oxydation de l'ammoniac
WO2010099970A1 (fr) * 2009-03-05 2010-09-10 Uhde Gmbh Procédé et dispositif pour contenir des particules de catalyseur recevant un courant
DE102013004341A1 (de) 2013-03-14 2014-09-18 Thyssenkrupp Uhde Gmbh Verfahren zur Oxidation von Ammoniak und dafür geeignete Anlage
CN110395488A (zh) * 2019-07-30 2019-11-01 西安交通大学 一种格架颗粒复合床堆积方法

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DE2226697A1 (de) * 1971-05-26 1973-01-04 North American Rockwell Verfahren und vorrichtung zur wasserstoff-sauerstoff-kombination
US3948610A (en) * 1972-06-05 1976-04-06 Imperial Chemical Industries Limited Catalyst beds for oxidizing ammonia to nitrogen oxides
US3985681A (en) * 1972-06-15 1976-10-12 Societe Chimique De La Grande Paroisse, Azote Et Produits Chimiques Catalyst for the oxidation of ammonia
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US4812300A (en) * 1987-07-13 1989-03-14 Sri-International Selective perovskite catalysts to oxidize ammonia to nitric oxide
WO1993024229A1 (fr) * 1992-06-01 1993-12-09 Pgp Industries, Inc. Feuilles poreuses pour utilisation en catalyse

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Title
CHEMICAL ABSTRACTS, vol. 111, no. 22, 27 November 1989, Columbus, Ohio, US; abstract no. 202883, WU, YUE ET AL: "Lathanum cerium cobalt oxide catalyst for ammonia oxidation" XP002092533 *

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102007026712A1 (de) 2007-06-06 2008-12-11 Uhde Gmbh Vorrichtung und Verfahren für katalytische Gasphasenreaktionen sowie deren Verwendung
JP2010528840A (ja) * 2007-06-06 2010-08-26 ウーデ・ゲーエムベーハー 触媒気相反応のための機器および方法ならびにその使用
US8394353B2 (en) 2008-10-20 2013-03-12 Johnson Matthey Plc Catalyst containment unit
WO2010046675A1 (fr) * 2008-10-20 2010-04-29 Johnson Matthey Plc Unité de confinement d’un catalyseur
DE102008059930A1 (de) 2008-12-02 2010-06-10 Uhde Gmbh Vorrichtung und Verfahren für katalytische Gasphasenreaktionen sowie deren Verwendung
EP2202201A1 (fr) 2008-12-23 2010-06-30 SÜD-CHEMIE CATALYSTS ITALIA S.r.l. Catalyseurs d'oxydation de l'ammoniac
US8435917B2 (en) 2008-12-23 2013-05-07 Sued-Chemie Catalysts Italia S.R.L. Ammonia oxidation catalysts
US10125020B2 (en) 2008-12-23 2018-11-13 Sued-Chemie Catalysts Italia S.Rl. Ammonia oxidation catalysts
WO2010099970A1 (fr) * 2009-03-05 2010-09-10 Uhde Gmbh Procédé et dispositif pour contenir des particules de catalyseur recevant un courant
DE102013004341A1 (de) 2013-03-14 2014-09-18 Thyssenkrupp Uhde Gmbh Verfahren zur Oxidation von Ammoniak und dafür geeignete Anlage
US10414654B2 (en) 2013-03-14 2019-09-17 Thyssenkrupp Industrial Solutions Ag Method for oxidizing ammonia and system suitable therefor
US11820653B2 (en) 2013-03-14 2023-11-21 Thyssenkrupp Industrial Solutions Ag Method for oxidizing ammonia and system suitable therefor
CN110395488A (zh) * 2019-07-30 2019-11-01 西安交通大学 一种格架颗粒复合床堆积方法

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NO20002522L (no) 2000-05-16
ZA9810270B (en) 1999-05-19
EP1034134A1 (fr) 2000-09-13
AU1046099A (en) 1999-06-07
AU733971B2 (en) 2001-05-31
CA2306780A1 (fr) 1999-05-27
NO20002522D0 (no) 2000-05-16
GB9724310D0 (en) 1998-01-14

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