DE102007024125A1 - Metal-doped zeolite for use as catalyst material for use in cleaning of exhaust gases, particularly for reduction of nitrogen oxides, has doping metal, which is present in zeolites as monomeric or dimeric species - Google Patents

Abstract

The metal-doped zeolite has doping metal, which is present in the zeolites as monomeric or dimeric species. The pores size of zeolites are 0.4-1.5 nm, and the doping metal is catalytically active and provided as 1-5 wt.% of metallic oxide. An independent claim is also included for a method for producing metal-exchanged zeolites, which involves manufacturing a zeolite in a closed reaction container with an aqueous suspension, increasing the pH value of the suspension 8-10 by adding ammonia in the form of ammonium hydroxide, and adjusting the oxygen content in the reaction container.

Description

The The present invention relates to a metal-doped zeolite, wherein the - catalytically active - doping metal isolated in the zeolite, d. H. as monomeric species and / or as dimers Species is present, as well as a method for producing such Zeolites and their use as catalyst material, in particular for the purification of exhaust gases, especially for the reduction of nitrogen oxides.

metal-doped Zeolites are known in the art and find wide Use as a catalyst material for the purification of Exhaust gases.

Due to the harmful impact of nitrogen oxide emissions on the environment, it is important to further reduce these emissions. Significantly lower NO _x emission limits for stationary and automotive exhaust gases than currently available are foreseen in the United States in the near future and are also under discussion in the European Union.

Around These limits can be achieved in the case of mobile combustion engines (Diesel engines) this no longer by internal engine measures be met, but only by an exhaust aftertreatment, for example with suitable catalysts.

The denitrification of combustion gases is also referred to as DeNO _x . In automotive engineering, selective catalytic reduction (SCR) is one of the most important DeNO _x techniques. As the reducing agent commonly used hydrocarbons (HC SCR) or ammonia (NH ₃ -SCR) and NH ₃ precursors such as urea (Ad-Blue ^®). Here, metal-exchanged zeolites (also referred to as 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 O ₅ based catalysts. In particular, iron-doped zeolites, by virtue of their high activity and resistance to sulfur under hydrothermal conditions, are good alternatives to the conventionally used vanadium catalysts. Conventional methods of doping zeolites with metals include, for example, methods such as liquid ion exchange, solid phase ion exchange, vapor phase ion exchange, mechanochemical processes, impregnation processes and the so-called ex-scaffolding procedures.

The US 5,171,553 discloses, for example, an ion exchange process in aqueous solution, wherein as support usually silicon-rich zeolites with Si / Al ratios of more than 5 to about 50 are used.

issues arise in particular when doping or introducing active Components, such. As iron, vanadium, cobalt and nickel in the Zeolites, since often different oxidation states of these catalytically active metals are present next to each other and not always the desired catalytically active species are obtained or the catalytically active species due to the parameters the doping process (oxygen, temperature, humidity, etc.) to catalytically inactive species.

Known is the doping of zeolites with iron by solid-state ion exchange ( EP 0 955 080 B1 ), wherein a mixture of the desired zeolite, a metal compound and an ammonium compound is sintered under a protective gas atmosphere, in particular re ductive inert gas atmosphere, so that metal-containing, in particular iron-doped, catalysts are obtained with increased long-term stability.

It However, it has been shown that virtually all known prior art cluster species of the catalytically active metals by the metal exchange in the interior of the zeolite, which are catalytically inactive, respectively extremely low catalytic activity. Under the term "Clusters" are thereby polynuclear bridged or unbridged Metal compounds understood that at least three of the same or contain different metal atoms. Metal exchanged zeolites, those in the interior of the zeolite skeleton no metal clusters have been detected are unknown.

task It was therefore an object of the present invention to provide a zeolite material this compared to the previously known zeolite a having increased catalytic activity.

These The object is achieved by a metal-doped zeolite, wherein the doping metal in the zeolite as isolated single atoms or cations (monomeric species) and / or as a dimeric species.

The metal-doped zeolite according to the invention (hereinafter also referred to as metal-exchanged zeolite is 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 dimeric catalytically highly active metal species in the pore structure or its framework whose structure forms the pores of the zeolite ,

The dimeric species can either be bridged be bridged (eg via O or OH atoms) or be unbridged, so have a metal-metal bond.

As a result, it is possible to work with much smaller amounts in metal doping (often also referred to as metal loading). Furthermore, the activity and selectivity of the zeolite of the invention over the known zeolites of the prior art is significantly increased. It has been found that, in general, the metal-doped zeolites according to the invention exhibit an increase in activity for each metal by about 30% in the reduction of the zeolites doped with the same metal, in which, as explained above, mostly metal clusters in the zeolite NO to N ₂ show. Moreover, inactive metal clusters lower the pore volume and prevent gas diffusion or lead to undesirable side reactions, which can advantageously also be avoided by the zeolites according to the invention.

The term "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, 1571 ) a crystalline substance from the group of aluminum silicates with spatial network structure of the general formula M ^{n +} _n [(AlO ₂ ) _x (SiO ₂ ) _y ] i ^t H ₂ O understood that consist of SiO ₄ / AlO ₄ tetrahedra, which are linked by common oxygen atoms to a regular three-dimensional network. The ratio of Si / Al = y / x is always ≥ 1 according to the so-called "Löwenstein rule", which prohibits the adjacent occurrence of two adjacent negatively charged AlO ₄ tetrahedra. Although there are more exchange sites for metals available at a low Si / Al ratio, the zeolite is becoming increasingly thermally unstable.

The zeolite structure contains voids 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 that 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 internal 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 manufacture (use or type of template, pH, pressure, temperature, presence of seed crystals). In the present case, it is particularly preferred if the Si / Al ratio of a zeolite according to the invention is in the range from 10 to 20 (corresponds to a ratio of SiO ₂ / Al ₂ O ₃ of 20-40).

In liquid exchange processes for the preparation of doped zeolites, there is a strong affinity for the exchange of polyvalent and heavy metal cations for lighter ones and in particular for hydrogen and / or NH ₄ ⁺ .

at the hydrated zeolites dehydration is usually done at temperatures below about 400 ° C and is the largest Part reversible.

The presence of 2- or 3-valent cations as a tetrahedral center in the zeolite framework of the zeolite receives a negati ve charge in the form of so-called anion sites in the vicinity of the corresponding cation positions are. 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 zigzag running channels, in others close behind the pore openings larger cavities, eg. B. in the Y and A zeolites, with the topologies FAU and LTA. In general, 10 and 12 "ring" zeolites are preferred according to the invention.

in principle In the context of the present invention, any zeolite, In particular, each 10 and 12 "ring" zeolite can be used. According to the invention, preference is given to zeolites with the Topologies AEL, BEA, CHA, EUO, FAO, FER, KFI, LTA, LTL, MAZ, MOR, MEL, MTW, LEV, OFF, TONE and MFI. Very particularly preferred zeolites the topological structures BEA, MFI, FER, MOR, MTW and TRI.

According to the invention zeolite-like materials can also be used, as for example in the US 5,250,282 are described, the disclosure of which is fully incorporated herein by reference. Further inventively preferred zeolite materials are mesoporous zeolite materials of silicates or aluminosilicates, which are known under the name M41S and described in detail in the US 5,098,684 and the US 5,102,643 are described, the disclosure of which is also fully incorporated by reference.

Further are so-called silicoaluminium phosphates (SAPOs) usable according to the invention, which originated from isomorphously exchanged aluminum phosphates.

It it is preferred that the pore sizes of the invention used Zeolites range from 0.4 to 1.5 nm, which is also due to the more favorable for monomeric or dimeric metal species steric conditions for the formation of monomeric or advantageously contributes to dimeric metal species in place of metal clusters.

typically, the metal content or the degree of exchange of a zeolite is decisive determined by the metal species present in the zeolite. there The zeolite can be used only with a single metal or with different ones Be doped metals.

It usually gives three different centers in zeolites, as so-called α-, β- and γ-positions which are the location of the exchange places (also referred to as "interchangeable positions"). All of these three positions are for reactants during accessible to the NH3-SCR reaction, especially during use from MFI, BEA, FER, MOR, MTW and TRI zeolites.

The so-called α-type cations show the weakest Binding to the zeolite skeleton and are in a liquid Ion exchange last filled. The occupation rate is from a degree of exchange of about 10% rising sharply with rising Metal content and total is around 10 to 50% at a degree of exchange to M / Al = 0.5. Form cations at this point very active redox catalysts.

The β-type On the other hand, cations show an average binding strength Zeolite framework, which in the liquid ion exchange, especially with small exchange rates, the most populated Position most effectively and catalyze the HC-SCR reaction. This position will be filled immediately after the γ position and their occupancy rate decreases from an exchange rate of around 10% with increasing metal content and is around 50 to 90% for a degree of exchange up to M / Al = 0.5. In the prior art is known that from a degree of exchange of M / Al> 0.56 typically only polynuclear metal oxides are deposited.

The γ type Cations are the cations with the strongest binding to zeolite framework and thermally most stable. you 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 catalytic most active cations.

The preferred metals for exchange and doping are catalytically active metals such as Fe, Co, Ni, Ag, Co, V, Rh, Pd, Pt, Ir, most preferably Fe, Co, Ni and Cu, which also bridged form dimeric species, as in the inventive Zeolites especially at high exchange rates mainly available.

Overall, the amount of metal calculated as the corresponding metal oxide 1 to 5 wt.% Based on the weight of the metal-doped zeolite. It is especially preferred that more than 50% of the exchangeable sites (ie α, β and γ sites) are replaced. Most preferably, more than 70% of interchangeable sites are replaced. However, vacancies should still remain, which are preferably Brønstedt acid sites. This is because NO is strongly absorbed at both the exchanged metal centers and also at ion exchange sites or at Brønstedt centers of the zeolite framework. In addition, NH ₃ preferentially reacts with the strongly acidic Brønstedt centers, the presence of which is therefore very important for a successful NH ₃ -SCR reaction. The presence of free residual exchange sites and / or Brønstedt acidic centers and the metal-exchanged lattice sites are 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.

by virtue of the risk of hydrothermal deactivation of metal-exchanged Zeolite, which is a dealumination and migration of metal precedes the ion exchange centers of the zeolite, it is preferred that the doping metals with aluminum as possible form a stable compound, since this promotes a dealumination becomes.

• a) Erhöhens des pH-Werts der Aufschlämmung auf einen Wert im Bereich von 8 bis 10, bevorzugt unter Verwendung von NH₄OH (Ammoniakwasser) und Einstellens des Sauerstoffgehalts im Reaktionsgefäß auf einen Wert von < 10%, bevorzugt < 5%
• b) Erniedrigens des pH-Werts auf einen Wert im Bereich von 1,5 bis 6
• c) Zugebens eines Metallsalzes und Umsetzens über einen Zeitraum von 1 bis 15 Stunden
• d) Abfiltrierens und Waschens des ausgetauschten dotierten Zeolithen

umfasst.The object of the present invention is further achieved by a process for producing a metal-exchanged doped zeolite according to the invention, wherein initially in a sealable reaction vessel an aqueous or water-containing slurry of a zeolite is prepared, and further the steps of

• a) Increasing the pH of the slurry to a value in the range of 8 to 10, preferably using NH ₄ OH (ammonia water) and adjusting the oxygen content in the reaction vessel to a value of <10%, preferably <5%
• b) lowering the pH to a value in the range of 1.5 to 6
• c) adding a metal salt and reacting for a period of 1 to 15 hours
• d) filtering off and washing the exchanged doped zeolite

includes.

By the reaction, in particular by the pH increase and lowering (the so-called "pH-guide" of the invention Method), it is achieved that a high degree of exchange of about 70-90% can be achieved without being unsuitable for catalysis Metal clusters in the metal-exchanged zeolite form what happened so far known from the prior art method, especially in the field the liquid exchange could not be achieved.

By the pretreatment, especially with ammonia, is the replacement rate and the extent of the exchange still increased. To Adjusting the oxygen content is the reaction mixture for stirred for about 1 to 60 minutes.

Surprisingly was found that even with a lowering of the pH to a Value of 1.5 to 6 in step b) of the invention Process highly exchanged zeolites (exchange limit approx. 90%) without metal clusters, although hitherto in the art It was also found and found to be at low pH in most of the catalytically active metals polynuclear hydroxo or form oxospecies that are catalytically inactive.

By repeated repetition of the method according to the invention the degree of doping can reach 100% of the exchangeable places be increased in the zeolite, although, as stated above, 90% is the preferred upper limit. It's the same, though in less preferred embodiments, possible that different metals are used for doping by the Choice of the metal salt in step c) is varied. To be favoured the above-mentioned salts of the catalytically active Metals such as their chlorides, sulphates, acetates, mixed ammonium-metal salts, Nitrates and soluble complex compounds used.

there The metal salt can be both in solid form as well as in form be added to a solution, wherein aqueous Solutions preferred because of easier workup are, however, nothing speaks against that, even in organic solvents or mixtures of aqueous or organic solvents dissolved metal salts are used.

typically, contains the resulting slurry 5 to 25 Wt.% Of zeolites to a good mixing by means of stirring to ensure higher levels of the mixture solidify.

The Increasing the pH is preferably carried out by adding a strong Base, most preferably in the form of ammonia water. Naturally For example, other suitable bases may also be used Bases such as NaOH or KOH due to their tendency to promote the formation of polynuclear hydroxo species with the metal salts are less advantageous.

The molar ratio of ammonia to zeolite is 0.01 to 0.1 to accurately adjust the pH to be able to len.

The acidification of the slurry is typically carried out by adding a mineral acid such as HCl, H ₂ SO ₄ , HNO _3, etc. Preferably, the acid is used whose anion is also the anion of the corresponding metal salt, which is then added. HCl is less preferred because of its high corrosivity in wastewater treatment.

All The pH is thereby particularly preferred in a range of 1.5 lowered to 3, which as stated above in the Contrary to the prior art, not to polynuclear hydroxo bridged metal cluster species leads.

To the acidification of the slurry is first heated to a temperature in the range of 80 to 100 ° C. and stirred for about 2 hours. The raised Temperature during the ion exchange advantageously leads to make the hydrate sphere of the metal ions smaller and so the exchange is accelerated.

Important is in the context of the method according to the invention, that the oxygen content in the reaction vessel during the reaction <10 and most preferably <5% is, as here also the formation of polynuclear oxygen- or hydroxo bridged metal species suppressed becomes.

The Reaction time for the metal exchange is about 2 to 8 hours, most preferably 3 to 5 hours. The powder obtained after reaction and doping is filtered off, if necessary, dried at more than 100 ° C, the temperature when drying at 250 ° C are not exceeded should, otherwise this leads to partial calcination.

A Calcination can range anywhere from 400 to 600 ° C preferably be carried out under inert gas.

Usually For example, any of the above-mentioned metal salt may be used Whether the metal is in a two-, three- or four-valued one Oxidation level is present, since usually in the Calcination sets a balance of redox couples. Most notably however, preferred are the divalent salts, especially in the case of iron salts, as these are typically less precipitous of sparingly soluble metal hydroxides and blocking the Tend zeolite pores. For higher quality iron salts should Therefore, the exchange time should not be too long, because it also precipitate more hydroxides.

Of the produced by the method according to the invention Zeolite is typically used in the purification of exhaust gases, especially in the reduction of nitrogen oxides.

The Invention is hereinafter based on embodiments explained in more detail without this as limiting to be understood.

General:

On the zeolites obtained according to the invention, diffuse reflection measurements were carried out by means of a Perkin-Elmer UV-VIS spectrometer with diffuse reflection and BaSO ₄ as reference UV-VIS-MIR. The evaluation of the absorption intensities was carried out according to the equation Schuster-Kubelka-Munk (often also called Kubelka Munk theory).

example 1

Making an iron-exchanged (or doped) zeolites

2 g of NH ₄ -ZSM5 (alternatively H-ZSM5 or Na-ZSM5 were used) were slurried in an amount of 10 to 15 wt.% Based on the aqueous solution in an aqueous solution and stirred at room temperature. Subsequently, ammonia in the form of ammonia water in a ratio of NH ₃ to zeolite of 0.04 was added, so that a pH of> 9 was set. The pH was a maximum of 10.

Subsequently the reaction vessel was closed, with inert gas rinsed and the atmosphere inside the vessel to an oxygen content of <5% set and for 20 min. maintained.

Subsequently, sulfuric acid in the form of dilute sulfuric acid concentration (25% by volume) was added, the ratio of sulfuric acid to zeolite being 0.05. The oxygen content was left at <5% and a pH of 4.0 was set. Subsequently, the acidified slurry was heated to a temperature of 90 ° C and then immediately solid FeSO ₄ .7H ₂ O added in a weight ratio of FeSO ₄ : 7H ₂ O to zeolite of 0.2. The pH was 3 and the reaction was carried out for 8 hours with stirring at an oxygen content of less than 5% in the reaction vessel.

Subsequently was the exchanged zeolite, which is a nearly white Color was filtered, and washed three times with distilled water and dried at 150 ° C. Calcination took place under Inert gas at 500 ° C for 3 hours.

The resulting product had 1.5 wt.% Fe ₂ O ₃ based on the total mass of zeolite.

UV-VIS:

The resulting iron-doped zeolite showed no bands in the 10-15,000 cm ^-1 wavenumber range associated with polynuclear Fe clusters (ie, more than 3 Fe atoms) which are low or absent in the SCR reaction.

In contrast, the iron-doped zeolite according to the invention exhibits strong bands in the wavenumber range of 25,000 to 30,000 cm ^{-1 associated} with iron oxide dimers (Fe-O-Fe) which are highly active in the SCR reaction. Similarly, the zeolite obtained in Example 1 showed bands in the wavenumber range between 30,000 and 50,000 cm ^-1 which are monomeric iron species located in the zeolite lattice or present as monomeric FeOH species which are also highly active for the SCR reaction.

One obtained by means of the iron zeolite prepared in Example 1 Catalyst thus has no polynuclear catalytically inactive Iron cluster on.

Example 2

Preparation of a cobalt-exchanged zeolites

• UV-VIS: 38–45.000 cm^–1 (m) (SCR aktive Monomere und dimere Co-Zentren), keine Banden bei 10 bis 15.000 cm^–1 (Clusterspezies).

Example 2 was carried out as Example 1. Only in place of iron sulfate (FeSO ₄ .7H ₂ O) was an appropriate amount of Co (NO ₃ ) ₂ or alternatively Co (acac) ₂ ((acacc =) acetylacetonate) used. In this case, instead of sulfuric acid, the corresponding amount of 0.01 M HNO _{3 was} used.

• UV-VIS: 38-45,000 cm ^-1 (m) (SCR active monomers and dimeric Co centers), no bands at 10 to 15,000 cm ^-1 (cluster species).

Example 3

Production of a copper-exchanged zeolites

• UV-VIS: 37–45.500 cm^–1 (m) (SCR aktive Monomere und dimere Co-Zentren), keine Banden bei 10–15.000 cm^–1 (Clusterspezies)

The synthesis was carried out as in Example 1, except that a corresponding amount of copper acetylacetonate solution was used as metal salt and also 0.01 M HNO 3 as acid.

• UV-VIS: 37-45,500 cm ^-1 (m) (SCR active monomers and dimeric Co centers), no bands at 10-15,000 cm ^-1 (cluster species)

Example 4

Making a silver-exchanged zeolites

The synthesis was carried out as in Example 1, except that AgNO _{3 was} used as the metal salt and 0.01 M HNO _{3 was} used as the acid.

Example 5

Production of a nickel-exchanged zeolites

The synthesis was carried out as in Example 1, except that Ni (NO ₃ ) _{2 was} used as the metal salt and 0.01 M HNO _{3 was} used as the acid.

Example 6

The catalyst obtained in Example 1 was tested in the reduction of NO to N ₂ .

there was the catalyst obtained according to the invention hydrothermally at 800 ° C for 12 hours in one Atmosphere with 10% steam aged, then pressed into shaped bodies and to a size of Sieved 0.4 to 0.8 mm.

Similarly, a comparative catalyst prepared according to the example of EP 955 080 B1 was hydrothermal aged in the same way. This comparative catalyst was obtained by solid-state ion exchange.

The exhaust composition for the comparative test was:
NO: 500 ppm
NH ₃ : 500 ppm
H ₂ O: 50 vol.%
SV (space velocity): 80,000
Rest N2

The test was carried out under standard test conditions. Table 1: conversion of NO to N ₂ temperature Fe zeolite Example 1 Comparative Fe-zeolite 200 ° C 35% 24% 350 ° C 95% 88% 500 ° C 92% 88%

As can be seen from Table 1, the conversion of NO to N ₂ when using a catalyst obtained according to the invention at 350 ° C is significantly higher than when using a comparative catalyst of the prior art. The temperature of 350 ° C is about the optimum temperature for the aforementioned DeNO _x method.

The Activity increase at 350 ° C was thus approx. 58%.

QUOTES INCLUDE IN THE DESCRIPTION

This list The documents listed by the applicant have been automated generated and is solely for better information recorded by the reader. The list is not part of the German Patent or utility model application. The DPMA takes over no liability for any errors or omissions.

Cited patent literature

• US 5171553 [0006]
• EP 0955080 B1 [0008]
• US 5250282 [0021]
• - US 5098684 [0021]
• - US 5102643 [0021]
• - EP 955080 B1 [0065]

Cited non-patent literature

• DS Coombs et al., Can. Mineralogist, 35, 1997, 1571 [0015]

Claims (21)

Metal-doped zeolite, wherein the doping metal is present in the zeolite as a monomeric and / or as a dimeric species. Zeolite according to claim 1, characterized in that that the zeolite is selected from the zeolites of the structural types AEL, BEA, CHA, EUO, FAO, FER, KFI, LTA, LTL, MAZ, MOR, MEL, MTW, LEV, OFF, TONE and MFI. Zeolite according to claim 2, characterized in that that the zeolite is selected from the zeolites with the Structural types BEA, MFI, FER, MOR, MTW, ERI. Zeolite according to claim 2 or 3, characterized the pore size of the zeolite is from 0.4 to 1.5 nm is. Zeolite according to claim 4, characterized in that that the doping metal is catalytically active. Zeolite according to claim 5, characterized in that that the metal is selected from the group of Fe, Co, Ni, Ag, Cu, V, Rh, Pd, Pt, Ir. Zeolite according to claim 6, characterized in that the doping metal is selected from the group consisting of Fe, Co, Ni, Cu. Zeolite according to claim 6 or 7, characterized the doping metal is calculated in an amount of 1 to 5% by weight present as metal oxide based on the total weight of the zeolite is. Zeolite according to claim 8, characterized in that that more than 50% of the exchangeable sites of the zeolite framework are occupied by the doping metal. Process for making a metal-exchanged Zeolites according to one of the preceding claims, wherein first in a sealable reaction vessel a aqueous slurry of a zeolite is further comprising the steps of a) Increasing the pH of the slurry to a value in the range from 8 to 10 and adjusting the oxygen content in the reaction vessel a value of <10%, b) Lowering the pH to a value in the range of 1.5 to 6 c) adding a metal salt and reacting over a period of 1 to 15 hours, d) filtering off and washing of the doped zeolite. Method according to claim 10, characterized in that the slurry contains 5 to 25% by weight of zeolite. Method according to claim 11, characterized in that that the increase in the pH in step a) by adding of ammonia takes place in the form of ammonia water. Method according to claim 12, characterized in that that the molar ratio of ammonia to zeolite one Value of 0.01 to 0.1. Method according to claim 13, characterized in that that the lowering of the pH in step b) by adding a Mineral acid takes place. Method according to claim 14, characterized in that that the pH is adjusted to a value in the range of 1.5 to 3 becomes. Method according to claim 14 or 15, characterized that after lowering the pH, the slurry heated to a temperature in the range of 80 to 100 ° C. becomes. Method according to claim 16, characterized in that during the exchange reaction in step c) the oxygen content is set to <5% in the reaction vessel. A method according to claim 17, characterized in that the zeolite obtained after step d) at a temperature of> 100 ° C is dried. Method according to claim 17 or 18, characterized that the process is performed several times. Method according to claim 18 or 19, characterized that the dried zeolite at a temperature of 400 to 600 ° C. is calcined. Method according to claim 20, characterized in that that the calcining is carried out under inert gas.