EP2162203A2 - Catalyseur pour gaz de fumée contenant de l'acide chlorhydrique - Google Patents

Catalyseur pour gaz de fumée contenant de l'acide chlorhydrique

Info

Publication number
EP2162203A2
EP2162203A2 EP08773818A EP08773818A EP2162203A2 EP 2162203 A2 EP2162203 A2 EP 2162203A2 EP 08773818 A EP08773818 A EP 08773818A EP 08773818 A EP08773818 A EP 08773818A EP 2162203 A2 EP2162203 A2 EP 2162203A2
Authority
EP
European Patent Office
Prior art keywords
zeolite
metal
catalyst
iron
species
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.)
Withdrawn
Application number
EP08773818A
Other languages
German (de)
English (en)
Inventor
Ingo Hanke
Arno Tissler
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 IP GmbH and Co KG
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 EP2162203A2 publication Critical patent/EP2162203A2/fr
Withdrawn legal-status Critical Current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
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/90—Regeneration or reactivation
    • 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
    • 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
    • B01J29/072—Iron group 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
    • 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
    • B01J29/076—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • 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
    • B01J38/00—Regeneration or reactivation of catalysts, in general
    • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
    • B01J38/42—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst using halogen-containing material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/207—Transition metals
    • B01D2255/20738—Iron
    • 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
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2045—Hydrochloric acid

Definitions

  • the present invention relates to a process for reactivating a catalyst containing an iron species-doped zeolite comprising the step of treating the catalyst with hydrogen chloride-containing gas. Furthermore, the invention relates to a reactivated catalyst which is obtained by means of the inventive method and their use for the treatment of exhaust gases from combustion processes, in particular for the treatment of waste gases from waste incineration plants, especially for the reduction of nitrogen oxides.
  • 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.
  • SCR Selective Catalytic Reduction
  • the reducing agents used are usually hydrocarbons (HC-SCR) or ammonia (NH 3 -SCR) or NH 3 precursors such as urea (AdBlue®).
  • HC-SCR hydrocarbons
  • NH 3 -SCR ammonia
  • AdBlue® NH 3 precursors
  • metal-exchanged zeolites also referred to as metal-doped zeolites
  • metal-doped zeolites have proven to be very active and can be used in a wide temperature range SCR catalysts. They are mostly non-toxic and produce less N 2 O and SO 3 than the usual V 2 Os based catalysts.
  • iron-doped zeolites owing to their high activity and resistance to sulfur under hydro-thermal conditions, are good alternatives to the vanadium catalysts conventionally used.
  • cluster species of the catalytically active metals are formed by the metal exchange in the interior of the zeolite, which are catalytically inactive, or whose presence greatly reduces the catalytic activity.
  • DE 38 41 990 discloses the use of molybdenum-containing Ca-doped zeolites, which are used in particular for use in flue gases from coal furnaces.
  • Methods for reactivating such catalysts of the catalysts for the denitrification of exhaust gases are also known and usually include the reduction of the inactivated catalysts or inactivated catalytically active species by means of a treatment with hydrogen (US 3,986,982).
  • EP 316 727 relates to the reactivation of noble metal-containing zeolites by means of a CCl 4 / ⁇ 2 / N 2 mixture.
  • the use of HCl is discouraged, since HCl gives poor results compared to CCI 4 and CFCl 2 and the reactivation is not completely successful.
  • cluster is understood to mean polynuclear bridged or unbacked metal compounds which contain at least three identical or different metal atoms. Metal-exchanged zeolites in which no metal clusters could be detected inside the zeolite framework are unknown.
  • This object is achieved by a process for reactivating a catalyst containing a metal species-doped zeolite comprising the step of treating the catalyst with hydrogen chloride-containing gas.
  • Hydrogen chloride can be used pure or with another gas such as N 2 . However, the gas contains no H 2 or organic chlorine compounds such as CCl 4 , CF 2 Cl 2, etc.
  • the catalyst can be treated in particular with pure HCl gas.
  • the metal species comprises iron, cobalt, copper or vanadium, most preferably iron.
  • metal species as used herein is further described below
  • the zeolite is also free of noble metals such as Pt, Pd, Rh, Ir, Ru, Os, Ag, Au.
  • the inventive method causes a conversion of the inactive metal species.
  • the catalytically inactive clusters are converted into active species, ie after the reaction, the metal-doped zeolite is substantially free of catalytically inactive or catalytically less active metal clusters, so that only monomeric (isolated species in the form of individual metal atoms or metal cations) or dimer catalytically highly active metal species in the pore structure or their Scaffold whose structure is formed by the pores.
  • Dimeric species are isolated species comprising two metal atoms, where the metal atoms may be either bridged (eg bridged by O atoms or OH group) or unbridged, i. have a metal-metal bond.
  • These are typically mixed oxo-hydroxo-metal species such as those described for iron in: M. Mauvezin et al., J. Phys. Chem. B 2001, 105, 928-035, or for other metals, for example, Verga et al. in "Catalysis by Microporous Materials” Elsevier 1005, pp. 665-672.
  • the process according to the invention significantly increases the activity and selectivity of the catalytically active metal-doped zeolite compared to the known zeolites of the prior art. It has been found that, in general, the metal-doped zeolites show an increase in activity over the prior art zeolites doped with the same metal, which, as explained above, are mostly metal clusters in the zeolite, ie not treated with HCl gas Metal by about 30% in the reduction of NO to N 2 show. This applies in particular to the Fe and Cu-containing zeolites. Moreover, inactive metal clusters reduce the pore volume and prevent gas diffusion or lead to undesirable side reactions, which can advantageously also be avoided by the process according to the invention.
  • zeolite is used in the context of the present invention as defined by the International Mineralogical Association (DS Coombs et al., Can. Mineralogist, 35, 1997, p. 1571) a crystalline substance from the group of aluminum silicates with 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).
  • 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 the present case, it is particularly preferred if the molar Si / Al ratio of an inventive according zeolites in the range of 10 to 20 is located. This corresponds to a ratio of SiO 2 / Al 2 O 3 of 20-40.
  • the presence of 2- or 3-valent cations as a tetrahedral center in the zeolite skeleton gives the zeolite a nega- tive charge in the form of so-called anion sites, in the vicinity of which the corresponding cation sites are located.
  • 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 SiO 4 / AlO 4 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. In general, 10 and 12 "ring" zeolites are erfmdungsgecut preferred.
  • any zeolite in particular any 10 and 12 "ring" zeolite, can be used in the present invention
  • preference is given to zeolites having the topologies AEL, BEA, CHA, EUO, FAO, FER, KFI, LTA, LTL, MAZ , MOR, MEL, MTW, LEV, OFF, TONE and MFI most preferably zeolites of the topological structures BEA, MFI, FER, MOR, MTW and TRI.
  • the pore sizes of the zeolites used in the process according to the invention are in the range from 0.4 to
  • the metal content or degree of exchange of a zeolite is significantly determined by the metal species present in the zeolite.
  • the zeolite can be doped with only one single metal or with different metals.
  • ⁇ there are usually three different centers in zeolites, referred to as ⁇ , ⁇ and ⁇ positions, which are the locations of the exchange sites (also referred to as "interchangeable.”
  • Reaction accessible especially when using MFI, BEA, FER, MOR, MTW and TRI zeolites.
  • ⁇ -type cations show the weakest binding to Zeolithgerust and are filled in a liquid ion exchange last.
  • the ⁇ -type cations show an average binding strength to the zeolite skeleton, which in the exchange of ions, especially at low exchange rates, represents the most occupied position and most effectively catalyzes the HC-SCR reaction.
  • the ⁇ -type cations are those cations with the strongest binding to the zeolite framework and thermally most stable. They are the least occupied position in liquid ion exchange, but are filled up first. Cations, especially iron and cobalt, at these positions are highly active and are the most catalytically active cations.
  • the preferred metals for exchange and doping in the present invention are catalytically active metals such as Fe, Co, Cu, V and mixtures thereof, most preferably Fe, which also form bridged dimeric species as used in the process of the invention Zeolites, in particular after treatment.
  • the amount of metal calculated as the corresponding metal oxide 1 to 5 wt.% Based on the weight of the metal-doped zeolite.
  • the weight percentages are based on a metal oxide, it is always meant the most stable metal oxides, ie, in the case of the iron oxide, Fe 2 O 3 is meant.
  • more than 50% of the exchangeable sites ie ⁇ , ⁇ and ⁇ sites
  • more than 70% of interchangeable sites are replaced.
  • vacancies should still remain, which are preferably Br ⁇ nsted acid sites. This is because NO is strongly absorbed both on the exchanged metal centers and also in ion exchange positions or Br ⁇ nstedt centers of the zeolite framework.
  • NH 3 preferably reacts with the strongly acidic Br ⁇ nstedt centers, the presence of which is therefore very important for a successful NH 3 -SCR reaction.
  • the presence of free residue exchange sites and / or Bronstedt acidic centers and the metal-exchanged lattice sites is therefore very particularly preferred according to the invention. Therefore, a degree of exchange of 70-90% is most preferred. At more than 90% degree of exchange, activity reduction was observed in the reduction of NO to N 2 and the SCR-NH 3 reaction.
  • the doping metals do not form a stable compound with aluminum, as this promotes dealumination.
  • the object of the present invention is also the provision of an activated catalyst based on a metal-doped zeolite which has catalytically active metal species which catalyze the selective catalytic reduction of nitrogen oxides in combustion processes.
  • the object is achieved by a catalyst prepared by a process described above for reactivating a catalyst containing a metal species doped zeolite which would be treated with hydrogen chloride gas.
  • the preferred metals of the metal species are the same as described above.
  • the activity and selectivity of Catalysis largely depends on the coordination of the metal species in the zeolite.
  • the catalytic activity is also the metal species, depending on the occupation of the ⁇ , ⁇ and ⁇ positions.
  • the object is further achieved by a catalyst for selective catalytic reduction obtained by the process according to the invention comprising a zeolite which contains a monomeric and / or dimeric species of a metal, the catalyst having a pore volume of 0.35 to 0.7 ml / g particularly preferably from 0.4 to 0.5 ml / g.
  • the catalyst according to the invention contains either monomeric or dimeric metal species or monomeric and dimeric metal species. Again, the preferred metal species are those described above.
  • the basis of this solution of the object on which the invention is based is the surprising discovery that zeolites containing inactive metal clusters can be converted into zeolites which contain catalytically active monomeric and / or dimeric metal species by contacting or gaseous hydrogen chloride.
  • the subject of the teaching according to the invention are therefore catalysts for the selective catalytic reduction from a zeolite which contains a metal species which are obtained after contacting the metal-containing zeolite with gaseous hydrogen chloride. So that the reaction with chlorinated toff can proceed Lithen in sufficient speed in accordance with the method of this invention inside the Zeo-, it is advantageous if the catalyst has the above-mentioned Po ⁇ renvolumina.
  • the metal species of the catalyst of the invention is selected from iron, cobalt, copper or Vana ⁇ dium or mixtures thereof, particularly preferably iron species.
  • the zeolite is advantageously selected from the zeolites of the structural types AEL, BEA, CHA, EUO, FAO, FER, KFI, LTA, LTL, MAZ, MOR, MEL, MTW, LEV, OFF, TON and MFI, in particular from the structural types BEA, MFI, FER, MOR, MTW and ERI.
  • the reaction of the hydrogen chloride gas can be carried out with sufficient reaction rates.
  • the catalyst ie the metal-doped zeolite present as a powder for selective catalytic reduction, has a BET surface area between 100 and 500 m 2 / g, preferably between 200 and 400 m 2 / g.
  • the pore size of the zeolite is between 0, 4 and 1.5 nm.
  • the metal in particular iron, is present in an amount of from 1 to 5% by weight, calculated as metal oxide, based on the total weight of the zeolite.
  • the metal for selective catalytic reduction is a 10 or 12 "ring" zeolite In this type of zeolite, a sufficient amount of metal can be incorporated and the gases to be reacted reach the active sites.
  • the catalyst for selective catalytic reduction after reactivation more than 50% of the exchangeable sites of the zeolite skeleton are coated with metal, in particular iron.
  • the catalysts are used for the treatment of exhaust gases, in particular for the reduction of nitrogen oxides in exhaust gases from gasification and combustion processes.
  • the catalysts are used for the treatment of waste gas from waste incineration plants. Since the catalyst is particularly suitable for use in the treatment of exhaust gases containing acidic constituents, the catalysts of the invention can be used precisely in plants in which the exhaust gas from the combustion processes is not subjected to acidic scrubbing.

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

Abstract

La présente invention concerne un procédé de réactivation d'un catalyseur qui contient des zéolithes dopées par une substance ferreuse, ledite procédé comprenant l'étape de traitement du catalyseur par un gaz qui contient du chlorure d'hydrogène. En outre, l'invention concerne un catalyseur réactivé obtenu à l'aide du procédé selon l'invention et son utilisation pour le traitement de gaz de fumée de processus de combustion, et en particulier pour le traitement de gaz de fumée d'installations d'incinération d'ordures, tout particulièrement pour la réduction des oxydes d'azote.
EP08773818A 2007-07-03 2008-07-02 Catalyseur pour gaz de fumée contenant de l'acide chlorhydrique Withdrawn EP2162203A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102007030895A DE102007030895A1 (de) 2007-07-03 2007-07-03 Abgaskatalysator für Salzsäure-haltige Abgase
PCT/EP2008/005406 WO2009003697A2 (fr) 2007-07-03 2008-07-02 Catalyseur pour gaz de fumée contenant de l'acide chlorhydrique

Publications (1)

Publication Number Publication Date
EP2162203A2 true EP2162203A2 (fr) 2010-03-17

Family

ID=39735503

Family Applications (1)

Application Number Title Priority Date Filing Date
EP08773818A Withdrawn EP2162203A2 (fr) 2007-07-03 2008-07-02 Catalyseur pour gaz de fumée contenant de l'acide chlorhydrique

Country Status (8)

Country Link
US (1) US20100221165A1 (fr)
EP (1) EP2162203A2 (fr)
JP (1) JP5285699B2 (fr)
KR (1) KR20100041778A (fr)
CN (1) CN101687187B (fr)
DE (1) DE102007030895A1 (fr)
HK (1) HK1141752A1 (fr)
WO (1) WO2009003697A2 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2517774A3 (fr) * 2007-04-26 2013-09-25 Johnson Matthey Public Limited Company Catalyseurs SCR de zéolithe de type ERI/métal de transition

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Publication number Priority date Publication date Assignee Title
DE102010055728A1 (de) * 2010-12-22 2012-06-28 Süd-Chemie AG Verfahren zur Umsetzung stickstoffhaltiger Verbindungen
JP5974631B2 (ja) * 2012-05-23 2016-08-23 株式会社豊田中央研究所 排ガス浄化用触媒及びその製造方法
EP3205398A1 (fr) 2016-02-12 2017-08-16 Hyundai Motor Company Procédé de préparation d'un catalyseur zéolite
KR101846914B1 (ko) * 2016-10-21 2018-04-09 현대자동차 주식회사 촉매 및 촉매의 제조 방법
RU2020102860A (ru) * 2017-07-11 2021-08-11 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Катализатор и способ его применения для конверсии nox и n2o

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Cited By (4)

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Publication number Priority date Publication date Assignee Title
EP2517774A3 (fr) * 2007-04-26 2013-09-25 Johnson Matthey Public Limited Company Catalyseurs SCR de zéolithe de type ERI/métal de transition
EP2517773A3 (fr) * 2007-04-26 2013-09-25 Johnson Matthey Public Limited Company Catalyseurs SCR de zéolithe de type LEV/métal de transition
EP2517775A3 (fr) * 2007-04-26 2014-05-21 Johnson Matthey Public Limited Company Catalyseurs SCR de zéolithe/métal de transition
US11478748B2 (en) 2007-04-26 2022-10-25 Johnson Matthey Public Limited Company Transition metal/zeolite SCR catalysts

Also Published As

Publication number Publication date
KR20100041778A (ko) 2010-04-22
JP2010531727A (ja) 2010-09-30
JP5285699B2 (ja) 2013-09-11
WO2009003697A3 (fr) 2009-03-19
US20100221165A1 (en) 2010-09-02
CN101687187A (zh) 2010-03-31
CN101687187B (zh) 2013-07-10
DE102007030895A1 (de) 2009-01-08
HK1141752A1 (en) 2010-11-19
WO2009003697A2 (fr) 2009-01-08

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