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WO2008151823A2 - Catalyseur zéolitique pour la dénitration de gaz d'échappement - Google Patents

Catalyseur zéolitique pour la dénitration de gaz d'échappement Download PDF

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Publication number
WO2008151823A2
WO2008151823A2 PCT/EP2008/004782 EP2008004782W WO2008151823A2 WO 2008151823 A2 WO2008151823 A2 WO 2008151823A2 EP 2008004782 W EP2008004782 W EP 2008004782W WO 2008151823 A2 WO2008151823 A2 WO 2008151823A2
Authority
WO
WIPO (PCT)
Prior art keywords
zeolite
catalyst system
catalyst
honeycomb body
exhaust gases
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/EP2008/004782
Other languages
German (de)
English (en)
Other versions
WO2008151823A3 (fr
Inventor
Roderik Althoff
Arno Tissler
Hans-Christoph Schwarzer
Ingo Hanke
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.)
Sued Chemie AG
Original Assignee
Sued Chemie AG
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 Sued Chemie AG filed Critical Sued Chemie AG
Publication of WO2008151823A2 publication Critical patent/WO2008151823A2/fr
Publication of WO2008151823A3 publication Critical patent/WO2008151823A3/fr
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
    • 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
    • B01D53/8628—Processes characterised by a specific catalyst
    • 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
    • B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
    • B01D53/94—Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
    • B01D53/9404—Removing only nitrogen compounds
    • B01D53/9409—Nitrogen oxides
    • B01D53/9413—Processes characterised by a specific catalyst
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/064—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof containing iron group metals, noble metals or copper
    • 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
    • B01J35/57—Honeycombs
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/50—Zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/90—Physical characteristics of catalysts
    • B01D2255/92—Dimensions
    • B01D2255/9202—Linear dimensions
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/42—Addition of matrix or binder particles

Definitions

  • the present invention relates to a DeNOx catalyst system for treating nitrogen oxides-containing exhaust gases comprising a bulk catalyst of a zeolite, wherein the bulk catalyst is an extrudate in the geometry of a honeycomb body.
  • Nitrogen oxides that are produced during combustion processes are among the main causes of acid rain and the associated environmental damage, and are the cause of the so-called summer smog, which leads to damage to health. Their emission should be prevented by removing them from the exhaust gases before they are released to the environment.
  • Sources of nitrogen oxide emissions into the environment are mainly motor vehicle traffic and incinerators, in particular power plants with furnaces or stationary internal combustion engines and waste incineration plants.
  • a reduction in NO x emissions can, for. B. in automotive engines by engine-side settings or power plants with boiler firing by using very pure fuels or by optimizing the combustion systems are achieved, but these firing measures both technical and economic limits set.
  • the aim is the most complete removal of NO x and N 2 O with little technical effort by novel catalyst systems.
  • the denitrification of exhaust gases is also referred to as DeNOx.
  • SCR selective catalytic reduction
  • Hydrocarbons (HC-SCR) or ammonia (NH 3 -SCR) or NH 3 precursors such as urea (AdBlue®) are usually used as reducing agents.
  • the principle is based on the fact that selected reducing agents selectively reduce nitrogen oxides in the presence of oxygen.
  • Selective means that the oxidation of the reducing agent is preferred (selective), which takes place with the oxygen nitrogen oxides and not with the molecular oxygen present in the exhaust much more abundant.
  • Ammonia or ammonia precursors have proven themselves as reducing agents with the highest selectivity.
  • urea is used in particular because of its non-toxicity, which likewise has very good solubility in water and can therefore simply be added to the exhaust gas as water solution to be metered.
  • NH 3 and isocyanic acid are formed in a thermolysis reaction:
  • catalysts consist either completely of the catalytically active component, which are what are known as bulk catalysts, which are also known to the person skilled in the art as unsupported catalysts, or the actual active component is applied to a carrier material, then it is referred to as coating catalysts.
  • Catalyst systems can be broadly distinguished in powder, shaped body and monolith catalysts, which are optionally coated.
  • the shaped-body catalysts mostly consist of ceramic particles or zeolites which are extruded into shaped bodies. Typical dimensions are here z.
  • B cylindrical moldings of 1.5 to 2.5 mm in diameter and 1.0 to 5.0 mm in length.
  • the ceramic materials are often alumina or silica.
  • These catalysts are mostly used in fixed bed reactors. Important parameters of fixed bed reactors are, in addition to the catalytic activity, the bulk density, the pressure loss properties and the surface of the catalyst. Furthermore, the design effort that is necessary for the preparation of the catalyst, an important economic parameter.
  • a honeycomb body is produced, which is optionally coated with a so-called washcoat.
  • the main body consists in this case mostly of a mineral ceramic, e.g. Cordierite, or a metal.
  • the washcoat is a powder suspension which i.a. Contains ceramic powder to obtain a large surface area. This powder suspension is applied to the honeycomb, dried and then impregnated with an active component and then activated by calcination.
  • Important parameters here, in addition to the catalytic activity, are the cell density, i. the number of channels per inflow unit and pressure loss at the catalyst. Other parameters are the surface of the catalyst and the design effort for the preparation of the catalyst.
  • the catalytically active component consists of the oxides of vanadium or titanium (V / Ti oxides), in a zeolite system.
  • V / Ti oxides vanadium or titanium
  • metal-exchanged zeolites also called metal-doped zeolites
  • SCR catalysts metal-exchanged zeolites
  • metal-doped zeolites have proven to be active SCR catalysts employable over a wide temperature range. They are mostly non-toxic and produce less N 2 O and SO 3 than the usual catalysts based on V 2 Os.
  • Both catalyst systems d. H.
  • the system based on zeolites and that based on V / Ti oxides are characterized in practice by, among other things, different catalyst geometries.
  • the catalyst packages are made from cylindrical extrudates.
  • honeycomb extrudates of various dimensions are typically used in which the channels have a square footprint.
  • Cylindrical extrudates are commonly used in fixed bed reactors with one or more catalyst beds.
  • Fixed bed reactors are characterized by a low geometric surface and because of the high flow resistance by a high pressure drop and by low design effort.
  • Honeycomb catalysts are commonly used in so-called frame reactors.
  • Frame reactors are characterized by a high surface area, by low pressure loss and by a high design effort in the production.
  • the object of the present invention was to provide a zeolite-based catalyst system for removing nitrogen oxides and nitrous oxide from an exhaust gas stream having a high surface area and exhibiting a low pressure drop, wherein the catalyst system is to be produced with a low design cost.
  • the object is achieved by a catalyst system for the treatment of nitrogen oxides-containing exhaust gases, which comprises a mass catalyst of a zeolite, wherein the mass catalyst is an extrudate which assumes the geometry of a honeycomb body and wherein the weight fraction of zeolite in the extrusion mass of the extrudate between 20 and 95%, preferably between 30 and 60%, and the zeolite is a catalytically active zeolite.
  • a honeycomb body is to be understood as meaning a shaped body which has parallel channels which are separated from one another by walls.
  • the channels may have an arbitrary polygonal base, e.g. a square, rectangular or hexagonal. Particularly preferred are rectangular base areas, as these simplify the production process and allow a space-saving arrangement of individual moldings in frame reactors. With the base of the channels, the area is meant, which is flowed through vertically.
  • the zeolite mass catalyst is characterized by a higher specific catalyst mass in the reaction space, by a significantly lower loss of catalytic activity due to attrition of the catalyst surface, as in the case of coating catalysts the case would be, and by a significantly simplified manufacturing process.
  • the reactors with catalyst system according to the invention have the advantage that the pressure loss, ie the pressure difference between the reaction gas at the reactor outlet and at the reactor inlet, is significantly lower is. Furthermore, the catalyst system according to the invention is characterized by an increased geometric surface on the reaction gas side, by less "fouling" of the reactor on the reaction gas side and by improved process gas flow.
  • the monolithic catalysts are additionally characterized by greatly reduced dust formation and thus triggered catalyst losses during loading and unloading of the reactor as well as the possibility of replacing parts of the catalyst bed in the operating time of the catalyst.
  • zeolite in the context of the present invention as defined by the International Mineralogical Association (D.S. Coombs et al., Can. Mineralogist, 35, 1997, 1571) is a crystalline substance from the group of aluminum silicates with a spatial network structure of the general formula
  • the zeolite structure contains cavities and channels characteristic of each zeolite.
  • the zeolites are classified according to their topology into different structures (see above). Splits.
  • the zeolite framework contains open cavities in the form of channels and cages which are normally occupied by water molecules and extra framework cations that can be exchanged.
  • An aluminum atom has an excess negative charge which is compensated by these cations.
  • the interior of the pore system represents the catalytically active surface. The more aluminum and the less silicon a zeolite contains, the denser the negative charge in its lattice and the more polar its inner surface.
  • the pore size and structure are determined by the Si / Al ratio, which determines most of the catalytic character of a zeolite, in addition to the parameters of preparation (use or type of template, pH, pressure, temperature, presence of seed crystals) ,
  • the negative charge is compensated by the incorporation of cations in the pores of the zeolite material.
  • the zeolites are mainly distinguished by the geometry of the cavities formed by the rigid network of SiO4 / AlO4 tetrahedra.
  • the entrances to the cavities are formed by 8, 10 or 12 "rings" (narrow, medium and large pore zeolites).
  • Certain zeolites show a uniform structure structure (eg ZSM-5 with MFI topology) with linear or zigzagging channels, in others close behind the Poreno réelleen larger cavities, z. B. in the Y and A zeolites, with the topologies FAU and LTA.
  • any zeolite in particular any 10 and 12 "ring" zeolite, can be used in the context of the present invention.
  • the metal content or degree of exchange of a zeolite is significantly determined by the metal species present in the zeolite. This allows the zeolite to be doped with only a single metal or with different metals.
  • the preferred metals for exchange and doping are catalytically active metals such as Fe, Ce, Co, Ni, Ag, V, Rh, Pd, Pt, Ir. According to the invention, very particular preference is given to zeolites containing iron or cobalt species.
  • ⁇ , ⁇ , and ⁇ positions which are the locations of exchange sites (also referred to as "interchangeable.”
  • Reaction accessible especially when using MFI, BEA, FER, MOR, MTW and TRI zeolites.
  • the free passage area flowing through the exhaust gas flow flowing perpendicularly is between 20 and 80%, preferably between 60 and 80% and most preferably about 70%.
  • This passage area is calculated from the quotient of the area freely flowed through by the exhaust gas flow divided by the inflow surface of the catalyst body.
  • the catalyst body is to be understood as the object which arises after extrusion and drying and immediately before insertion into a frame. Too large a passage area would make the catalyst body unstable because the walls would be too narrow and therefore unstable. at Too small a passage area, the pressure loss of the process or combustion gas would be too large over the Formkorper.
  • the cell density of the honeycomb body is between 1 and 200 per cm 2 , preferably between 2 and 50 per cm 2 .
  • the cell density is calculated from the number of channels per start-up unit.
  • the honeycomb body contains a mixture of zeolite, binder, filler and additive.
  • the zeolite represents the catalytically active component.
  • the proportion by weight of zeolite in the honeycomb body is, as stated above, between 20 and 95%, preferably between 30 and 60%.
  • the binder is made of an inorganic material, e.g. Boehmite, which allows the shaping process.
  • the weight fraction of the binder is between 5 and 60%, preferably between 20 and 40%.
  • the filling material consists of a porous carrier material, e.g. Alumina, with a weight fraction of the honeycomb body of 0 to 40%, preferably between 10 and 30%.
  • the additive consists of a material which affects the physical properties of the honeycomb or the mixture of components e.g. a Tixotropiersch with a weight proportion between 0 and 10%. The proportion by weight is calculated from the quotient of the mass of zeolite divided by the total mass of the honeycomb body.
  • An extrudable mass is produced by mixing zeolite with water, binders and possibly inert filler material and additives. Binders and additives are chosen so that they influence the properties of the mixture, eg the flow properties, so that the extrusion process and the drying process tion and hardening process during production is made possible.
  • the honeycomb body is in the form of a cylinder.
  • the honeycomb body has a diameter of 10 to 500 mm, preferably of 200 to 400 mm, and / or a height of 10 to 500 mm, preferably of 200 to 400 mm.
  • the height of the honeycomb body is here and below equivalent to the passage of the exhaust gas flow through the honeycomb body.
  • the height of the honeycomb body is crucial for the conversion of nitrogen oxides contained in the exhaust gas or nitrous oxide contained in the exhaust gas, since the contact time increases with the height of the honeycomb body , Too small highs mean too little turnover and too high altitudes are on the one hand not economical and on the other hand associated with a higher pressure loss.
  • the preferred dimensions of the honeycomb bodies are particularly suitable for the use of the inventive catalyst systems for the treatment of exhaust gases from internal combustion engines.
  • the honeycomb body of the catalyst system according to the invention has a cuboid shape.
  • the cuboid honeycomb body has a side length of 10 to 500 mm, preferably 50 to 200 mm, and / or a height of 10 to 500 mm, preferably 150 up to 300 mm.
  • the advantage of cuboid honeycomb bodies lies in special installation requirements and in a space saving.
  • the advantages of the dimensions are the same as the pre ⁇ parts of the dimensions of the cylindrical honeycomb body.
  • the catalyst systems according to the invention are used for the catalytic treatment of exhaust gases from combustion or incineration plants as well as plants for the production of nitric acid, adipic acid or caprolactam.
  • the catalyst systems of the present invention find use for the catalytic removal of nitrogen oxides from exhaust gases from gasification and combustion processes, e.g. Waste incineration plants or for denitrification of motor vehicle exhaust gases.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Catalysts (AREA)
  • Exhaust Gas Treatment By Means Of Catalyst (AREA)

Abstract

L'invention concerne des systèmes catalytiques alternatifs d'élimination des NOx servant à traiter des gaz d'échappement contenant des oxydes d'azote, le catalyseur comprenant un catalyseur massique composé d'un zéolite et ce catalyseur massique étant un produit d'extrusion présentant une géométrie de corps alvéolaire. L'invention concerne en outre des utilisations du système catalytique selon l'invention.
PCT/EP2008/004782 2007-06-15 2008-06-13 Catalyseur zéolitique pour la dénitration de gaz d'échappement Ceased WO2008151823A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102007027676.3 2007-06-15
DE102007027676A DE102007027676A1 (de) 2007-06-15 2007-06-15 Zeolithischer Katalysator zur Entstickung von Abgasen

Publications (2)

Publication Number Publication Date
WO2008151823A2 true WO2008151823A2 (fr) 2008-12-18
WO2008151823A3 WO2008151823A3 (fr) 2009-04-30

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PCT/EP2008/004782 Ceased WO2008151823A2 (fr) 2007-06-15 2008-06-13 Catalyseur zéolitique pour la dénitration de gaz d'échappement

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DE (1) DE102007027676A1 (fr)
WO (1) WO2008151823A2 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020030204A1 (fr) 2018-08-07 2020-02-13 Vysoká Škola Báňská - Technická Univerzita Ostrava Procédé de préparation d'un catalyseur pour l'élimination d'oxyde nitreux de gaz industriels usés et catalyseur préparé par ce procédé

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0205813A3 (fr) * 1985-04-22 1988-09-21 Klaus Rennebeck Catalyseur, en particulier pour purification de gaz d'échappement, procédé et dispositif pour sa fabrication
DE3841990A1 (de) * 1988-12-14 1990-06-21 Degussa Verfahren zur reduktion von stickoxiden aus abgasen
ATE127707T1 (de) * 1991-11-02 1995-09-15 Degussa Verfahren zur oxidativen reinigung von stickoxide enthaltenden abgasen.
WO1994027709A1 (fr) * 1993-05-28 1994-12-08 Engelhard Corporation Catalyseur utilise dans la decomposition de l'oxyde azote
DE19721440A1 (de) * 1997-05-21 1998-11-26 Degussa Verfahren zur Reinigung eines mageren Abgases und Katalysatorsystem hierfür
EP1242183A1 (fr) * 1999-12-28 2002-09-25 Corning Incorporated Compositions supports de catalyseur zeolithe/alumine et procede de preparation associe
CN1153619C (zh) * 1999-12-29 2004-06-16 康宁股份有限公司 高强度和高表面积催化剂、催化剂载体或吸附剂组合物
DE102006020158B4 (de) * 2006-05-02 2009-04-09 Argillon Gmbh Extrudierter Vollkatalysator sowie Verfahren zu seiner Herstellung

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020030204A1 (fr) 2018-08-07 2020-02-13 Vysoká Škola Báňská - Technická Univerzita Ostrava Procédé de préparation d'un catalyseur pour l'élimination d'oxyde nitreux de gaz industriels usés et catalyseur préparé par ce procédé

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Publication number Publication date
WO2008151823A3 (fr) 2009-04-30
DE102007027676A1 (de) 2008-12-18

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