WO2006009453A1 - Garnissage de catalyseur, reacteur a lit fixe structure et utilisation de ceux-ci - Google Patents

Garnissage de catalyseur, reacteur a lit fixe structure et utilisation de ceux-ci Download PDF

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Publication number
WO2006009453A1
WO2006009453A1 PCT/NO2004/000223 NO2004000223W WO2006009453A1 WO 2006009453 A1 WO2006009453 A1 WO 2006009453A1 NO 2004000223 W NO2004000223 W NO 2004000223W WO 2006009453 A1 WO2006009453 A1 WO 2006009453A1
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Prior art keywords
catalyst
packing
reactor
particles
bed reactor
Prior art date
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PCT/NO2004/000223
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English (en)
Inventor
Javier PERÉZ-RAMÍREZ
Original Assignee
Yara International Asa
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Priority to PCT/NO2004/000223 priority Critical patent/WO2006009453A1/fr
Publication of WO2006009453A1 publication Critical patent/WO2006009453A1/fr

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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
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B01D53/8631—Processes characterised by a specific device
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8634—Ammonia
    • 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
    • B01J19/2485—Monolithic 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
    • B01J35/56—Foraminous structures having flow-through passages or channels, e.g. grids or three-dimensional monoliths
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/402—Dinitrogen oxide
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/322—Basic shape of the elements
    • B01J2219/32203—Sheets
    • B01J2219/32265—Sheets characterised by the orientation of blocks of sheets
    • B01J2219/32268—Sheets characterised by the orientation of blocks of sheets relating to blocks in the same horizontal level
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/322—Basic shape of the elements
    • B01J2219/32203—Sheets
    • B01J2219/32265—Sheets characterised by the orientation of blocks of sheets
    • B01J2219/32272—Sheets characterised by the orientation of blocks of sheets relating to blocks in superimposed layers
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/322—Basic shape of the elements
    • B01J2219/32279—Tubes or cylinders
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/322—Basic shape of the elements
    • B01J2219/32282—Rods or bars
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/322—Basic shape of the elements
    • B01J2219/32296—Honeycombs
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/32—Details relating to packing elements in the form of grids or built-up elements for forming a unit of module inside the apparatus for mass or heat transfer
    • B01J2219/324—Composition or microstructure of the elements
    • B01J2219/32466—Composition or microstructure of the elements comprising catalytically active material
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/10—Capture or disposal of greenhouse gases of nitrous oxide (N2O)

Definitions

  • the invention concerns a structured catalyst packing, a fixed bed reactor for catalytic applications and use of the catalyst.
  • Packed-bed reactors have been traditionally used in a number of catalytic applications. In this reactor type, the catalyst particles are stacked in a random orientation.
  • Two major drawbacks are identified in conventional packed-bed reactors: high-pressure drop and low catalyst effectiveness. More efficient structured reactors have been developed, including the monolith reactor, the lateral-flow reactor, the parallel-passage reactor, the cross-flow reactor, and the bead-string reactor. As common aspects, these reactors have a low- pressure drop and dust resistance compared to traditional randomly packed reactors. However, they show a serious disadvantage: a low ratio of active catalyst volume to total reactor volume.
  • the bead-string reactor is characterised by the fact that the catalyst material is attached to parallel wires ordered in a reactor.
  • the reactor elements of a bead string reactor are manufactured by stringing commercially available hollow extrusions or annular pellets on a wire or rod; or by extruding a catalyst support material around a wire or a rod.
  • Such a reactor is described in Dutch patent application 9000454.
  • This type of reactor has high porosity, i.e. a low catalyst amount-to-reactor volume ratio.
  • the catalyst element consists of parallel rods of catalyst-containing material, which material has been provided around a rod-shaped support through pressing in a die.
  • the invention further relates to structured catalyst packing consisting of elements manufactured according to this method.
  • the individual catalyst elements could be arranged relative to each other in such a manner that fluid particles cannot move in a straight line through the packing.
  • this reactor type has a very high porosity.
  • International patent application WO 9948604 describes a structured reactor with a framework that divides the reactor into a plurality of elongated cells or chambers within the reactor of different shapes.
  • the framework may be porous or non-porous.
  • the cells are filled with catalyst particles. This configuration only allows vertical flow through the reactor.
  • the object of the invention is to obtain a reactor and catalyst packing with low-pressure drop and high catalyst volume to reactor volume ratio. Another object is to find catalyst packings suitable for NH 3 oxidation and N 2 O decomposition.
  • Figure 1 shows different catalyst shapes applied.
  • Figure 2A shows closely packed pellets of hexagonal shape and Figure 2B shows a packing of pellets with square shape.
  • Figure 3A shows line-up cylinders in hexagonal packing
  • Figure 3B shows shifted cylinders in hexagonal packing
  • Figure 3C illustrates line-up cylinders in cubic packing, while shifted cylinders are shown in Figure 3D.
  • Figure 4 shows bed porosity for different reactor configurations.
  • Figure 5 shows a basket used in pilot plant tests with random fixed-bed reactor A and the reactor according to the invention C.
  • the middle picture, B shows a mixed configuration.
  • Figure 6 shows the influence of the reactor configuration on the bed porosity, pressure drop, and catalytic performance in the high-temperature ammonia oxidation and in direct N 2 O decomposition.
  • the invention thus concerns a structured catalyst packing that comprises one or more catalyst elements consisting of a horizontal layer of individual catalyst particles closely packed where each catalyst particle has one or more parallel flow channels arranged vertically.
  • the layers could be aligned or shifted compared to each other allowing for both vertical and radial flow of gas through the packing. Radial flow could also be obtained by changing the size and location of the channels in each layer. In this way radial flow could be obtained in cubic, hexagonal and cylindrical aligned particles as well.
  • the catalyst particles are preferably cylindrical, hexagonal or square.
  • a catalyst particle up to 10 mm diameter will have 2-7 flow channels.
  • the number of flow channels will be dependent on the particle size.
  • a large amount of flow channels is preferred to increase the surface area, but it should not be more than to still maintain the strength of the particles.
  • a preferred configuration is cylindrical catalyst particles arranged in cubic packing.
  • Another preferred configuration is cylindrical catalyst particles or catalyst bodies arranged in hexagonal packing.
  • the open space between the particles in this packing has an area in the same order as each flow channel in the particle. This allows a very uniform flow. Every second layer of catalyst particles could be shifted.
  • the invention also concerns a fixed-bed reactor with a catalyst packing as described above.
  • Preferred use of such a reactor is for NH 3 oxidation and N 2 O decomposition.
  • NH 3 oxidation it is preferred to use a catalyst packing with aligned channels in all layers, while for N 2 O decomposition it is preferred to use a catalyst packing with shifted channels or a packing where the size and/or location of the channels are changed in each layer to allow both vertical and radial flow through the packing.
  • the invention described here focuses on the development of a novel type of reactor with structured catalyst packing for heterogeneous catalysis, the so-called modular structured fixed-bed reactor (MOSFIBER).
  • MOSFIBER modular structured fixed-bed reactor
  • MOSFIBER is a fixed-bed reactor with ordered catalyst material of different shapes. This configuration displays the advantages of monolithic reactors (low-pressure drop), but having a high catalyst amount-to-reactor volume ratio, even higher that in traditional fixed-bed reactors with random packing of catalyst particles. Hydrodynamics, kinetics, and transport phenomena can be decoupled in this configuration, which is highly advantageous in catalytic applications.
  • Figure 1 shows different catalyst shapes applied, in the form of a square, hexagon or cylinder.
  • Several reactor configurations with different geometrical characteristics can be considered by structuring the pellets in different ways. The examples are carried out using equilateral pellets (length and diameter are the same, ca. 10 mm and holes (flow channels) of ca. 2 mm), but any dimension of particles could be used. The number of holes or flow channels of the pellets is variable, and also dependent on the size, but it should have more than one. Compared to a monolith, the main difference is a smaller size of the pellets (denoted as miniliths) and that a conventional pressing process can manufacture them. A monolith requires extrusion when the whole monolith is to be made of the active phase, which is technically challenging.
  • a ceramic monolith (often cordierite) can be wash coated with a thin layer of catalyst.
  • the catalyst amount is even lower.
  • Figure 2 and 3 shows the arrangement of pellets.
  • Figure 2A shows closely packed pellets of hexagonal shape and
  • Figure 2B shows a packing of pellets with square shape.
  • the holes in the pellets are aligned so macroscopically the reactor is a monolithic reactor.
  • no monolith can be extruded with the flexibility in dimension of pellets (particularly regarding hole size).
  • Figure 3A thus shows line-up cylinders in hexagonal packing, while Figure 3B shows shifted cylinders in hexagonal packing.
  • Figure 3C illustrates line-up cylinders in cubic packing, while shifted cylinders are shown in Figure 3D.
  • the orientation and packing of the catalyst can be changed as shown in Figure 3, so the reactor characteristics ⁇ e.g. porosity) and thus performance can be tuned to resemble anything between a conventional randomly distributed fixed-bed reactor and a monolithic reactor.
  • Figure 4 shows bed porosity as a function of reactor configuration for different materials.
  • Column 1-4 illustrates catalyst materials according to this invention compared to a random bed in column 5 and monoliths in columns 6-7.
  • the figure shows that the structure in MOSFIBER leads to reactors with low porosities, ranging from 20-40 %, enabling high amounts of catalyst per reactor volume. These values are considerably lower than a random fixed-bed reactor and dramatically differ from the high porosities in monolithic reactors, up to 80 % depending on cell density and wall thickness.
  • Figure 5 shows the catalyst basket used in the pilot tests. It was used cylindrical pellets with diameter about 10 mm and 7 flow channels.
  • the catalyst amount (or number of pellets) in the pictures as shown in Figures 5a and 5c is exactly the same (ca. 2 kg), but the reactor volume in Figure 5a is obviously higher (due to the higher porosity).
  • the top view in Figure 5b nicely illustrates the degree of structure in MOSFIBER as compared to fixed-bed configurations normally used in industrial gas-solid applications.
  • Figure 6 shows the influence of the reactor configuration on the bed porosity, pressure drop, and catalytic performance in the high-temperature ammonia oxidation and in direct N 2 O decomposition.
  • Experiments were carried out both for a random fixed-bed reactor and MOSFIBER with shifted cylindrical pellets and hexagonal packing and with cubic pellets. The results are also compared with monoliths. These have a limited amount of catalytic material, as the catalytic material is applied as a wash coating to the ceramic structure.
  • the volume of the monolithic reactor was the same as for MOSFIBER. Accordingly, all the catalysts are compared in terms of reactor volume.
  • the porosity in MOSFIBER configurations is considerably lower as compared to random fixed-bed reactor and monolithic reactor.
  • the monolith used in this example was that of 200 cpsi in Figure 4.
  • the relative pressure drop is very similar to that of the monolith and 5 times lower as compared to a random fixed-bed reactor. This is due to the presence of structure.
  • the performance of MOSFIBER in both catalytic applications investigated is superior to the other reactor configurations. Again, the poor performance of the monolithic reactor is a consequence of the limited amount of catalyst per reactor volume.
  • MOSFIBER thus combines a tunable and low porosity (high W ca t/V rea cto r ) and a low pressure drop (in the same order as monoliths). Which MOSFIBER configuration to be applied depends on the intrinsic characteristics of the reaction and reactor space available in retrospective applications.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Biomedical Technology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Analytical Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Materials Engineering (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Catalysts (AREA)

Abstract

L'invention concerne un garnissage catalyseur structuré comprenant un ou plusieurs élément catalyseurs constitués d'une couche horizontale de particules individuelles étroitement serrées les unes contre les autres. Chaque particule de catalyseur comprend un ou plusieurs canaux d'écoulement parallèles disposés verticalement. Les couches peuvent être décalées les unes relativement aux autres ou la dimension et/ou l'emplacement des canaux d'écoulement de chaque couche peut être modifiée de manière à permettre aussi bien un écoulement vertical qu'un écoulement radial à travers le garnissage. Les particules de catalyseur peuvent être cylindriques, hexagonales ou carrées, et comprennent normalement de 2 à 7 canaux d'écoulement pour des particules présentant un diamètre jusqu'à 10 mm. Le garnissage de type cubique ou hexagonal peut remplacer les particules cylindriques. Ce réacteur catalytique structuré est utilisé de préférence pour la décomposition de N2O ou l'oxydation de NH3.
PCT/NO2004/000223 2004-07-19 2004-07-19 Garnissage de catalyseur, reacteur a lit fixe structure et utilisation de ceux-ci WO2006009453A1 (fr)

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PCT/NO2004/000223 WO2006009453A1 (fr) 2004-07-19 2004-07-19 Garnissage de catalyseur, reacteur a lit fixe structure et utilisation de ceux-ci

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Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009005371A1 (fr) * 2007-07-04 2009-01-08 Yara International Asa Procédé servant à produire des catalyseurs et catalyseur produits par celui-ci
EP2202201A1 (fr) * 2008-12-23 2010-06-30 SÜD-CHEMIE CATALYSTS ITALIA S.r.l. Catalyseurs d'oxydation de l'ammoniac
DE102009037882A1 (de) 2009-01-13 2010-07-15 Linde Aktiengesellschaft Vorrichtung und Verfahren zur Zersetzung von Lachgas in einem adiabaten Festbettreaktor
JP2013519501A (ja) * 2010-02-12 2013-05-30 ジョンソン、マッセイ、パブリック、リミテッド、カンパニー 触媒構造体
JP2013537847A (ja) * 2010-09-08 2013-10-07 ジョンソン、マッセイ、パブリック、リミテッド、カンパニー 触媒製造方法
WO2015181492A1 (fr) * 2014-05-30 2015-12-03 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Catalyseur sous forme d'un monolithe avec un réseau de canaux
US9579628B2 (en) 2015-04-15 2017-02-28 Air Products And Chemicals, Inc. Perforated adsorbent particles
WO2017089231A1 (fr) 2015-11-27 2017-06-01 Basf Se Monolithe catalyseur modulaire
CN114713145A (zh) * 2020-12-22 2022-07-08 中国石油化工股份有限公司 一种级配催化剂的装填方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4086158A (en) * 1976-09-24 1978-04-25 Gulf Research & Development Company Process for upgrading solids-containing liquid hydrocarbon oils
US4297248A (en) * 1978-04-05 1981-10-27 Sakai Chemical Industry Co., Ltd. Method for packing catalysts
EP0073150A2 (fr) * 1981-08-20 1983-03-02 United Kingdom Atomic Energy Authority Dispositif catalytique
US4743578A (en) * 1985-11-13 1988-05-10 Imperial Chemical Industries Plc Ceramic structures
JPH078706A (ja) * 1993-06-28 1995-01-13 Miyauchi Tsuneko 気液接触用充填物
US5725810A (en) * 1995-11-29 1998-03-10 Sulzer Chemtech Ag Packing for a counterflow high pressure column
DE10208711A1 (de) * 2002-02-28 2003-09-25 Basf Ag Keramisches Packungselement

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4086158A (en) * 1976-09-24 1978-04-25 Gulf Research & Development Company Process for upgrading solids-containing liquid hydrocarbon oils
US4297248A (en) * 1978-04-05 1981-10-27 Sakai Chemical Industry Co., Ltd. Method for packing catalysts
EP0073150A2 (fr) * 1981-08-20 1983-03-02 United Kingdom Atomic Energy Authority Dispositif catalytique
US4743578A (en) * 1985-11-13 1988-05-10 Imperial Chemical Industries Plc Ceramic structures
JPH078706A (ja) * 1993-06-28 1995-01-13 Miyauchi Tsuneko 気液接触用充填物
US5725810A (en) * 1995-11-29 1998-03-10 Sulzer Chemtech Ag Packing for a counterflow high pressure column
DE10208711A1 (de) * 2002-02-28 2003-09-25 Basf Ag Keramisches Packungselement

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3335781A1 (fr) * 2007-07-04 2018-06-20 YARA International ASA Procédé de fabrication de catalyseurs et catalyseurs associés
AU2008271375B2 (en) * 2007-07-04 2012-12-13 Yara International Asa Method for producing catalysts and catalysts thereof
WO2009005371A1 (fr) * 2007-07-04 2009-01-08 Yara International Asa Procédé servant à produire des catalyseurs et catalyseur produits par celui-ci
EA018747B1 (ru) * 2007-07-04 2013-10-30 Яра Интернэшнл Аса Способ получения катализаторов
US9084987B2 (en) 2007-07-04 2015-07-21 Yara International Asa Method for producing catalysts and catalysts thereof
EP2202201A1 (fr) * 2008-12-23 2010-06-30 SÜD-CHEMIE CATALYSTS ITALIA S.r.l. Catalyseurs d'oxydation de l'ammoniac
US10125020B2 (en) 2008-12-23 2018-11-13 Sued-Chemie Catalysts Italia S.Rl. Ammonia oxidation catalysts
DE102009037882A1 (de) 2009-01-13 2010-07-15 Linde Aktiengesellschaft Vorrichtung und Verfahren zur Zersetzung von Lachgas in einem adiabaten Festbettreaktor
JP2013519501A (ja) * 2010-02-12 2013-05-30 ジョンソン、マッセイ、パブリック、リミテッド、カンパニー 触媒構造体
JP2013537847A (ja) * 2010-09-08 2013-10-07 ジョンソン、マッセイ、パブリック、リミテッド、カンパニー 触媒製造方法
US9272264B2 (en) 2010-09-08 2016-03-01 Johnson Matthey Plc Catalyst manufacturing method
US9278338B2 (en) 2010-09-08 2016-03-08 Johnson Matthey Plc Catalyst manufacturing method
US9839907B2 (en) 2010-09-08 2017-12-12 Johnson Matthey Plc Catalyst manufacturing method
FR3021556A1 (fr) * 2014-05-30 2015-12-04 Air Liquide Catalyseur sous forme d'un monolithe avec un reseau de canaux
WO2015181492A1 (fr) * 2014-05-30 2015-12-03 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Catalyseur sous forme d'un monolithe avec un réseau de canaux
US9579628B2 (en) 2015-04-15 2017-02-28 Air Products And Chemicals, Inc. Perforated adsorbent particles
WO2017089231A1 (fr) 2015-11-27 2017-06-01 Basf Se Monolithe catalyseur modulaire
RU2722375C2 (ru) * 2015-11-27 2020-05-29 Басф Се Модульные каталитические монолиты
US10974964B2 (en) 2015-11-27 2021-04-13 Basf Se Modular catalyst monoliths
CN114713145A (zh) * 2020-12-22 2022-07-08 中国石油化工股份有限公司 一种级配催化剂的装填方法

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