DE1442888B2 - Process for making a cracking catalyst - Google Patents

Description

3 4

X-aluminosilicates are described in US-PS 28 82 244 are for example gels of silicon dioxide, zirconium

ben. The production of the Y-type is in the BE-PS oxide, aluminum oxide, magnesium oxide and combination

5 77 642. nations of the same with each other, clays, aluminum

Another important synthetic crystalline oxide, metals and refractories.

Zeolite, which does not have a corresponding natural form, 5 It was also found that the activity of

is the zeolite A. The production of this crystalline crystalline aluminosilicate catalyst in question

Aluminosilicate is in US-PS 28 82 243 and lysatoren by a water vapor treatment

29 82 612. driving can be reduced and that a regulated

Other suitable synthetic crystalline zeolites, steaming can be applied to catalysts

which are useful in the context of the invention are 10 to be achieved with any desired degree of activity

for example zeolite Y, zeolite B, zeolite D, zeolite. The degree of dampening of a particular

lith E, zeolite F, zeolite G, zeolite H, zeolite K-G, catalyst to achieve a desired activity

Zeolite J, Zeolite L, Zeolite M, Zeolite K-M, Zeotätshöhe is largely of the type of catalytic

lith Q, zeolite R, zeolite S, zeolite T, zeolite U, depending on the material.

Zeolite W, zeolite Z and others. 15 For example, the crystalline aluminosilicate

Highly suitable crystalline aluminosilicate catalyst in an atmosphere which can be synthesized, for example, between about 5 % and about 100% water vapor, at Tempeden by using sodium X molecular sieve at temperatures of about 260 to 871 ⁰ C and below Press ion exchange with a solution of rare earths ranging from subatmospheric pressure to chlorides until the sodium content is treated up to about 20 up to several hundred atmospheres 1.0 to 1.5 weight percent sodium is reduced until the desired modification of the property - And about 25 percent by weight of rare earth ions, shafts of the catalyst is reached.
calculated as SE ₂ O ₃ are introduced. Cations that are suitable to replace the

The aluminosilicate zeolites can also be converted into the original H cations of a crystalline zeolite

or acid form can be converted into the water 25 by ion exchange processes for the purpose of modification

Substance ions occupy the cation sites. Such of its catalytic properties can be used

Conversion can, for example, by ion conversion, are for example: Ba, Ca, Ce, Li, Mg, Ag,

exchange with ammonium ions, followed by an Er- Sr, Zn, La, Pr, Nd, Pm, Sm, Eu, Gd, Tb, Dy, Ho, Er,

heating to expel NH ₃ , or by using Tm, Yb, Lu, Mn, Be, Ti, Zr, Hf, V, Cr, Fe, Co, Ni,

regulated acid leaching with a hydrochloric acid solution or 30 Cu, Cd, Al, Sn, Pb. A relatively small one

a similar reagent can be achieved. In general, the amount of polyvalent metal cations is improved

nen the Η-form is more stable in materials, which for example the structural stability of the crystalline

Have SiO ₂ / Al ₂ O ₃ ratios of 3.5 or higher. Aluminosilicates into which it has been introduced,

Usable catalysts are also to a considerable extent, especially with regard to the

Combination of ion exchange treatments - thermal and water vapor stability of the material,

testifies. For example, the crystalline aluminum can be used as an example of activity regulation by ionic

Minosilicates by acid leaching into the H or acid exchange can be a crystalline aluminosilicate

form and then with a solution of the 13X-type with a mixture of rare earths

Rare earth metal salts are ion-exchanged, chlorides of the type described above are base-exchanged

about catalysts, such as those exchanged with rare earths and water, about a rare earth aluminosilicate

Substance-exchanged mordenite, with rare earths and with a rare earth content of about 20 to 25%,

Hydrogen exchanged synthetic faujasite calculated as SE ₂ O ₃ . This material has

X- or Y-type and many other usable freshly prepared ions have a very high relative

exchanged catalysts. There can also be activity, however the relative activity can do this

more than one type of metal cation for ion exchange 45 material by controlled steaming, e.g. B. by

the crystalline aluminosilicates are used and the treatment is carried out in a steam atmosphere

Order of the ion exchange treatments vari- 5 to 40 hours at 704 ⁰ C to more suitable heights

be ized. For example, the acid treatment can be lowered.

for the introduction of hydrogen ions from an ion exchange The original metal ion can after various exchange treatment for the introduction of metal cations 50 NEN base exchange methods partially or completely precede or follow. are constantly being replaced by other metal cations.

Investigations have led to the conclusion that the original cations can alternatively be used

that the extremely high activities of the crystalline next partially or completely in the acid form

Aluminosilicates by combining the crystal! - converted and then exchanged with other metal cations.

The aluminosilicate component can be exchanged for less than 55. The relative concentrations of the

active or inert material, by water vapor reagents and the treated material, the size

treatment, by exchanging the original of the particles and the reaction conditions can

Metal cations, usually sodium, potassium, and all can be changed and adjusted to desired

Calcium, to achieve other metal cations or water degrees of replacement or ion exchange, Substance ions and can be modified by calcination 60 It is possible to change the properties of crystalline

can. To modify aluminosilicates by calcining,

In the process according to the invention, that is, by heating at high temperatures, support materials of different activity levels can be found below the sintering temperature of the particular aluminum turn, and any amount of the silicate can be used over different periods of time,
65 Furthermore, it is possible to induce crystalline aluminosilicates of a desired level of activity in the finished catalyst with a suitably reduced activity. Suitable support materials which can be used in a combination of the above-specified catalysts of this type to produce working methods, for example, a

5 6

Sodium Y-aluminosilicate material with a mixture The precalcination of the crystalline aluminosilicate of calcium and hydrogen ions can also be base-exchanged by high temperature spray drying to form a calcium-hydrogen Y zeolite with aluminosilicate particles after formation. Produced at a relatively high activity. For example, wet with rare earth ions can then be reduced the activity of this material by 5 exchanged particles of synthetic faujasite pre-carrier dilution to be calcined by spray-drying it in a stream of air catalytic material with a relative conversion of the an inlet temperature of 538 ⁰ C to produce lung activity, which has about twice the and an outlet temperature of 246 ° C. Others of the original NaY material and the working methods for the precalcination are, for example, use in existing cracking processes, such as the calcination of the crystalline aluminosilicate. over a period of 3 hours at 593 ° C in air

It is important that the fluidized catalytic bed or, in a water vapor atmosphere at 1.05 kg / cm ² , material has a particle size such that the particles of the resulting rare earth particles suspended in the nuidizing medium exchanged crystalline aluminosilicates become one can. Although the exact size 15 by weighing mean particles through the particles can vary up to about 40 µ depending on the conditions, then the reactor and the type of conversion used in preparation for the formation of the concomitant feed may vary, particles are settled Catalyst slurried in water, about 20 to 200 microns in size, is generally satisfactory for suspension in fluidized beds 20 (b) making the carrier-forming solutions.

When producing cracking catalysts according to General, the gels can be produced The invention is an overactive crystalline aluminum by making solutions of salts of yellowing oxides minosilicate component with a relatively in-neutralized. In a preferred embodiment active carrier component combined. The invention is a matrix made of a silicon dene satisfactory working methods used for the production of dioxide-aluminum oxide gel. This will of the composite cracking catalysts usually evolved by neutralizing a solution of and these generally include the monosodium silicate made with an acid solution. the Incorporation of finely divided aluminosilicate particles in acid solution may also contain a salt, e.g. B. Aluein Carrier material, which is preferably made of a 3 ° miniumsulfat, which the aluminum oxide content of the Silica-alumina gel is made up of. Gels brings about. Accordingly, as a preliminary stage of

A preferred one. Procedure for generating gel formation initially prepares gel-forming solutions.

Cracking catalysts according to the invention include the gel-forming solutions for use in the

following general steps: Production of a silica-alumina gel

35 generally comprise an aqueous solution of

(a) Preparation of the aluminosilicate component sodium silicate and an aqueous solution which is a

Contains acid and aluminum sulphate.

A suitable crystalline aluminosilicate is obtained.

methods for incorporation into the carrier material are prepared, for example in the

selects, with a preferred starting material a 40 US-PS 27 01 793, 28 59 184, 29 41 961, 30 03 951 and

X-type synthetic faujasite. This Kataly 30 23 172 are described.

The carrier material can also be treated by contact with a solution of

Rare-earth chlorides are ion-exchanged in order to be deactivated by water vapor

to make at least about 75% of the sodium content of the more susceptible. This can be done through education

remove initial molecular sieve. 45 of a carrier with a high silicon dioxide / aluminum

The catalytic properties of the material are carried out in a deminium oxide ratio, since such materials

which can be more easily deactivated by steam treatment on these materials.

Position further modified. the. The wearer's susceptibility to dis-

It has been found that maintenance of activation by steam treatment can also

Crystallinity of kata prepared according to the invention 50 can be increased by having a relatively

by precalcining the crystalline large amount of sodium in the silicon dioxide-aluminum

Aluminosilicate is improved. For example, if left miniumoxydgel.

the crystalline aluminosilicate in a proportion- The activity of the carrier can also be dispersed prior to the moderately inactive carrier material agreement with the highly active aluminosilicate composite, e.g. B. in a silica-alumina gel, 55 nent can be reduced by being catalytically inert, it has been found possible to incorporate the crystallinity of the fines in the support.
Aluminosilicates, ζ. B. a rare earth element instead of steam annealing of the synthetic faujasite, a product to reduce the activity of the carrier, such as calcining the material to drive off water in the procedure described above, thereby forming a more stable structure ⁶ ° it should be preferable to use a carrier of low activity and to avoid the loss of crystallinity during re-use and thereby rapid drying that involves steam, for example by spraying. Suitable carrier material drying, wet processing, steaming and scrap materials with low activities are, for example, making as little as possible. The calcination of clays, aluminum oxides, hydrated metal oxides, is carried out by heating the crystalline aluminosilicate ⁶ 5 silicon dioxide gel, aluminum oxide gel, thorium oxide zeolite after ion exchange to a temperature gel, alkaline earth oxide-silicon dioxide gels, gels or never below the sintering temperature of the earth and in general the sintering temperature of cerium or Zirconium oxide in the range from 260 to 871 ⁰ C. gel, hafnium oxide gel, tin oxide gel, titanium oxide gel, etc.

(c) Introduction of the crystalline aluminosilicate composite (e) formation of fluidized bed catalyst particles

nente in the gel-forming solutions ^ -oju . λι_ · λ λ-

According to the preferred procedure, the

In the process according to the invention, the catalyst beads are then stirred or beaten in water In addition, it is generally preferable to form a paste or a slurry in the particle in the manufacture of the sator crystalline aluminosilicate component finely divided and completely dispersed by adding the composition Slurries of aluminosilicate particles to which are gelled. This aqueous slurry is then preferred to introduce forming solutions. Spraying is usually carried out around microspheres of the catalyst the addition to the sodium silicate solution under permanent form, which for use in catalytic Stirring or agitation carried out in order to make the partial fluid bed processes suitable, Chen in a fully dispersed state. The spraying of the catalyst-forming sludge

The addition of overactive crystalline or aluminous solutions can be by a number of methods Silicate particles can also be added to the acid solution or, e.g. B. by spray molding the droplets in the silicate and acid solutions after air or by guiding the sprayed droplets into mixture, but done before the gel is formed. 15 cocurrent, countercurrent, semi-countercurrent or circular die to the aluminosilicate and gel matrix stream with respect to a stream of a drying gas, added fine particles can be up to a size. Spray molding can be with or without drying

to a mean particle determined by weighing. In each case the diameter is used of about 40 microns. Special spray for the formation of small approximately spherical Advantages can also be obtained by adding fine particles 20 of the catalyst. If significantly below about 7 microns and preferably large amounts of moisture are to be removed range of 0.3 to 3.0 microns can be achieved. the spray is usually in a stream of a

It has also been found that heated drying gas produces good results.

can be achieved by using a hydrogel. When spray drying using a

turns, z. B. a silicon dioxide-aluminum oxide 25 mode of operation with semi-countercurrent are the hydrogel droplets, the one sprayed up to the range of about 6 to 11 surfaces in a chamber, which set and preferably in the range of about drying gas and in which the droplets partly-7.0 has a pH value of up to 10.0. The pH can be dried wisely, whereupon the droplets can be adjusted by the addition of alkalis, is provided, downwards in countercurrent to an uptake. B. of sodium hydroxide, ammonium hydroxide, 30 increasing stream of a drying gas down to calcium oxide or calcium hydroxide, magnesium oxide trickle.

or magnesium hydroxide etc. if the carrier is too The drying medium in the spray drying acid is. If the hydrogel is too alkaline, the device can be acidified from superheated steam or acid salts such as ammonium chloride, understand; this has a tendency to turn the catalytic itself will. The hydrated carrier can be obtained in the form of aluminosilicate, Washed essentially free of soluble salts ... _, ,,,, _,. ,,

and the sodium content should be less than post-formation treatments

0.5% sodium (on a dry solids basis) and after the fluidized bed catalyst particles through

preferably less than 0.2% sodium. Spray molding, spray drying or the like.

It has been found that the application of a high 4 ° denier, it may be desirable to use the particles to subject the pH value in the hydrogel carrier to certain additional treatments before spraying, drying opens the structure of the carrier and the. According to a preferred mode of operation, the physical properties of the catalyst compounded catalyst particles with water, steam treated. For example, if the

45 composite particles about 5 percent by weight

(d) Beading of a rare earth exchanged synthetic

X-type faujasites and 95 percent by weight of one

The slurry of aluminosilicate particles and fines comprising silica-alumina gels, if fines are used, is then dispersed in the solutions forming the composition at 649 ° C for 24 hours in the carrier gel; the latter are attenuated 5 ° steam of 1.05 kg / cm ^2, are mixed and become a hydrogel solidify Alternatively, the water vapor treatment on left containing therein the aluminosilicate for 16 hours at 704 ⁰ C in water vapor at atmosphäverteilt. The hydrogel formation can be carried out under constant pressure in order to achieve the desired modification of the catalytic properties of the solutions and dispersed aluminosilicate particles 55 of the product.

forms into droplets and the droplets by an In addition to ion exchange and water vapor

Settling or solidification medium, e.g. B. an oil column, treatments can let the composite catalyst sink. After formation, the acidity of the hydrogel is also regulated by other chemical factors in order to manipulate the properties of the product gel, to influence it in order to disactivate it and to create such a ^{setting time} , to improve the selectivity or to reduce the rate of solidification during the passage c'er table properties of the material in another way to modify droplets through the solidification column at the end. For example, it can come together. used a catalyst to modify its properties

After washing or rinsing, the 'th η be the further Behanc- ⁶ S a Calciumhydroxydlösung are treated with a calcium acetate-acetic acid solution or with this manner resulting beads, subjected lungs, z. B. the additional ionization A suitable method for generating additional

Exchange treatment with rare earth chloride or compound overactive fluidized bed catalyst ammonium solutions. gates, which is an essential embodiment of the

Forming the present invention comprises incorporating the crystalline aluminosilicate into a synthetic one Gel, e.g. B. a silica-alumina gel, which is produced by precipitation.

Such a process generally involves the formation of a silica gel by neutralization an alkali silicate solution with an acid, while the pH of the gel is on the alkaline side is held. Solutions of sulfuric acid, acetic acid, hydrochloric acid, carbonic acid and other acids can be used to neutralize the silicate solution. The silica hydrogel is then mixed with an aqueous acidic solution of a salt, which leads to the formation of aluminum oxide in is able to. Hydrous alumina is then precipitated within the silica gel to form a silica-alumina gel. After precipitation, the gel is recovered and sprayed, Spray drying or other procedures to fluidizable particles, e.g. B. microspheres, shaped.

In the conventional procedure, the silica-alumina gel produced by this process is used recovered by filtration, and it can then be pre-sprayed or otherwise shaped be washed into fluidized bed particles. In some processes, the washing stage precedes the spraying omitted.

The particles can also be washed after they have been used to remove residual ions, z. B. sodium or sulfate ions, have been sprayed, and they can then be subjected to a further drying stage.

In a variation of this process, the aluminum oxide can be contained in the pores of the silicon dioxide gel precipitated from solutions of salts in which aluminum is present in the cation, z. B. aluminum sulfate, and also from solutions of salts in which aluminum is present in the anion is e.g. B. sodium or potassium aluminate. The use of separate solutions of this type leads to a double precipitation of alumina within the silica gel.

The crystalline aluminosilicate particles can be added at any stage prior to the formation of the final particles the composition in the silica-alumina gel carrier be incorporated. The preferred way to incorporate the overactive Component comprises adding a slurry of crystalline aluminosilicate particles to the alkali silicate solution. However, good results are also obtained by using the crystalline aluminosilicate particles in the The course of subsequent stages of the process clogs.

The crystalline aluminosilicate particles can be added, for example: (1) with the acid solution, (2) to the acidified silicate solution before it has solidified into a gel, (3) to the silicon dioxide hydrogel, after this has been precipitated, (4) to the silica gel after adding the aluminum salt solution, (5) to the silicon dioxide gel after precipitation of hydrous aluminum oxide within the pores of the silica gel, (6) to the silica-alumina gel after recovery by filtration and (7) to the silica-alumina gel after filtration and washing in those working methods that include a washing stage before spraying use.

The fluidized bed size particles produced by this process can also be one or more Ion exchange treatments after they have been formed. If such downstream exchange treatment is used, the catalyst particles, z. B. sprayed Microspheres, usually washed to remove residual ions from the exchange treatment and then dried.

ίο The registration is given below on the basis of examples explained in more detail.

example 1

10,450 g of sodium silicate, consisting of an approximately 30% strength aqueous solution of Na ₂ O (SiOa) ₃ ^, were mixed with 62.58 l of water, and the mixture was heated to 48.9 ° C. Thereafter, the pH of the mixture by adding 304 cm ³ of 96, l% sulfuric acid over a period of 30 minutes to 10.4 has been lowered, after which the mixture to 6O ⁰ C. and was maintained at this temperature for 3 hours . The pH of the mixture was then ^{reduced to 4.9 by adding a further 520 cm 3 of} the acid in order to cause the precipitation of silicon dioxide.

To the mixture having a pH of 4.9 was added 162 g of the rare earth exchanged zeolite of Y type in which three quarters of the cation sites were occupied by rare earth cations and that for 15 minutes of calcination at 649 ° C, was added in the form of a 5% suspension in an aqueous solution of rare earth chloride, whereupon it was homogenized and spray-dried. The product in the form of microspheres was washed twice with water and then continuously exchanged in a column with 56.8 liters of a 5% ammonium sulfate solution. The thus-exchanged material was washed free of chloride and sulfate, and then dried at 121.1 ⁰ C., 2 587 g of a catalyst was obtained which contained the exchanged with rare earths, ammonium zeolite Y in a Siliciumdioxydträger.

Example 2

1860 g of koalin (86% solids content) were mixed with 49.91 of water, and then 8,360 g of sodium silicate [an approximately 30% aqueous solution of Na ₂ O (SiO ₂ ) ₃ , 3] were added to the clay-water Mixture added, whereupon the mixture was heated to 48.9 ° C. The pH was then reduced to 10.2 by the addition of 234 cm ^{3 of} 96.1% strength sulfuric acid over a period of 30 minutes, after which the mixture was heated to 60 ° C. and held at this temperature for 2 hours. The pH of the mixture was then reduced by the addition of a further 418 cm ³ of the acid to 4.7 to cause precipitation of silica.

To the mixture having a pH of 4.7 was added 216 g of the rare earth exchanged zeolite Y, in which three quarters of its cation sites were occupied by rare earth cations and that for a period of 15 minutes of calcination at a temperature of 649 ° C had been subjected, in the form of a 5% suspension in an aqueous solution of rare earth chloride added, whereupon it was homogenized and spray-dried. The product in the form of

Microspheres were washed twice with water and then continuously exchanged in a column with 75.7 liters of a 5% ammonium sulfate solution. The thus-exchanged material was washed free of chloride and sulfate, and then dried at 121.1 ⁰ C, with 2 783 g of a catalyst was obtained, the clay-silica support containing the exchanged with rare earths, ammonium zeolite Y in one.

Example 3

8360 g of sodium silicate, consisting of an approximately 30% strength aqueous solution of Na ₂ O (SiO ₂ ) 3.3, were mixed with 36.3 l of water, and 370 g of NaOH were then added to the silicate-water mixture. A well stirred suspension of 1600 g of A-3 alumina in 3800 cm ³ of water with a content of 16.0 g of a dispersant-water mixture was added thereto, the silicate was heated and then the whole to 48.9 ⁰ C; at this point the pH was 11.3. The pH was then ^{reduced to 10.0 by adding 730 cm 3} of 98% strength sulfuric acid over a period of 30 minutes, whereupon the mixture was heated to a temperature of 60 ° C. and held at this temperature for 3 hours. Thereafter, the pH of the mixture was ^{lowered to 4.5 by adding another 186 cm 3 of} the acid to cause the precipitation of silicon dioxide.

To the mixture having a pH of 4.5 was added 456 g of the rare earth exchanged zeolite Y, in which three quarters of its cation sites were occupied by rare earth cations and that of calcination over a period of 15 minutes at a temperature of 649 ° C had been subjected to in the form of a 10% strength

ίο suspension in an aqueous solution of rare earth chloride was added, whereupon the mixture was homogenized and spray-dried using spray dryer inlet and outlet temperatures of 343 and 138 ° C, respectively. The product in the form of microbeads was washed twice with water and then continuously exchanged in a column with 1141 of a 5% ammonium sulfate solution. The thus-exchanged material was washed free of chloride and sulfate, and then dried at 121.1 ⁰ C, whereby a catalyst was obtained which contained the exchanged with rare earths, ammonium Y zeolite in a support of silica and alumina.
The effectiveness of the catalysts prepared according to Examples 1, 2 and 3 after various heat treatments in the flowing catalyst cracking of gas oil can be seen from the table below.

Catalyst treatment Flow catalyst cracking test test 5 Conversion C ₅ ⁺ gas oil Wide-cut MC gas oil Dry coke Physical Properties Pores Ge (Bench FCC test) 5 lung (WCMCGO) gas volume . grabbed 10 density 496 ° C (925 ⁰ F), 5 cat / oil, 5 WHSV Entire C ₁ Ge Ge Upper Rare 5 Volume Volume weight weight area- Earth Y 5 percent percent percent percent area cm ³ / g g / cm ³ 10 Ge Volume weight 65.5 47.4 percent 7.6 5.7 m ² / g 1.00 0.40 Calcined in air - percent 72.5 53.7 8.2 5.6 0.80 0.44 3 hours each at 649 ° 5 82.7 50.9 10.8 11.2 0.75 0.46 example 1 C. 5 16.1 377 Example 2 10 26.9 21.5 17.4 3.7 2.6 267 0.93 0.42 Example 3 68.6 52.7 25.5 7.4 4.5 284 0.77 0.47 940.5 ⁰ C 82.2 60.8 8.8 7.7 0.68 0.48 example 1 5 2.7 297 Example 2 5 14.6 255 Example 3 10 19.5 253 Muffled 53.9 45.4 4.9 2.2 0.89 0.42 4 hours - 760 ⁰ C - 67.0 57.0 5.6 2.1 0.77 0.45 Oatu 66.7 55.6 6.0 2.7 0.70 0.50 example 1 10.5 272 Example 2 12.2 228 Example 3 31.9 27.1 13.7 3.6 1.7 179 0.88 0.41 5 hours - 760 ⁰ C- 58.4 49.8 5.0 2.1 0.74 0.54 1.05 atm 0.68 0.47 example 1 4.2 228 Example 2 10.3 184 Example 3 141

Claims (2)

1 2 which the alkali ions of a crystalline aluminum patent claims: silicate zeolite with uniform pore openings between 6 and 15 Å against polyvalent metal ions 1. Process for the production of a Krackkata- be exchanged, the product of soluble lysators, in which the alkali ions of a crystal anions are washed free, thermally activated and with linen aluminosilicate zeolite with uniform pore metal compounds or metals of group VI openings between 3 and 13 Å against others and VIII of the periodic table is united.
Cations are exchanged to at least 75%. Such a hydrocracking catalyst consists of which the product is dried, ^{heated to a temperature of a combination of a cracking catalyst with a 260 to 871 0} C and a support material io hydrogenation / dehydrogenation catalyst. According to the Belgian patent which is unified, characterized by the hydrogenation / Dehyn et, that the cation-exchanged product drierungskatalysator with the cracking catalyst, one after heating in a carrier material made of a calcined, rare-earth metal ions inorganic oxide gel or clay and exchanged zeolite , the composite material can optionally be combined by ion exchange »5. after washing, another ion exchange The known method for producing a submits, dries and optionally with tem- Hydrocracking catalyst is not suitable that the Temperatures of 260 to 871 ⁰ C with water vapor underlying the present invention treated. to solve. A cracking catalyst that has a reduced 2. Use of a according to claim 1 herge ao cation (namely an elemental metal or a provided catalyst for cracking carbon-corresponding metal compound) is a Hydrogen. very poor cracking catalyst. It is actually a hydrocracking catalyst. " Generally, the eligible ones have As crystalline aluminosilicate zeolites the following general formula The invention relates to the manufacture of a Cracking catalyst, which is particularly suitable for fluidized bed M ₂ O-Al ₂ O -YSiO -ZH ₂ O and fluidized bed process is suitable. ^ There are various fluidized bed and fluidized bed 30 Catalysts known, the generally fine part- here η is the valence of the metal cation M, Y is Chen of catalytically active material, which is the number of moles of silicon dioxide, and ZH ₂ O is for suspension, the water of hydration in a stream of a medium. are suitable. The most important properties for the crystalline aluminosilicate zeolites of the foregoing Cracking catalysts like this are abrasion-resistant, have the same structure, and are sometimes also sized as molecular sieves Porosity, satisfactory catalytic ^ acti- can be drawn by removal of the hyvity and persistent catalytic properties. drainage water to be activated; if you are in this The previously known cracking catalysts, activated in ways, they have places that are used to promote who are particularly capable of catalytic fluidized bedding of catalytic conversions, processes are suitable, but do not yet correspond to 40. After the dehydration, the alumino- all requirements. Silicates are highly porous, and they have numerous The object of the invention is to create a surface cavities and internal pores which the drive to make a cracking catalyst that connect voids. These pores have essentially is particularly suitable for fluidized bed processes borrowed constant diameter, in general and the excellent activity and improved 45 range from 3 to 13 angstrom units; the exact physical properties in particular in terms of size depends on the composition and the the abrasion resistance, the controlled particle size structure of the particular aluminosilicate. and density and has good selectivity, in order to obtain the desired cracking properties, low tendency to form coke and good reactor and the original cations of the aluminum Excellent regenerator stability. 50 silicates, usually sodium, potassium and / or calcium According to the invention, this object is achieved by subjecting cium to an ion exchange. It has by a process for the production of a cracked kata- shown that the ion exchange of the original lysators, in which the alkali ions of a crystalline ion have a particularly beneficial effect on the kata-aluminosilicate zeolite with uniform pore-opening cracking properties of the crystalline aluminum has between 3 and 13 Å against other cations to 55 minosilicates. at least 75% replaced, the product There are a considerable number of natural dried to a temperature of 260 to 871 ⁰ C crystalline zeolites, and among these has become When heated and combined with a support material, faujasite is considered a particularly useful material for which is characterized in that the cationic preparation of the catalysts according to the invention exchanged product after heating in a 60 turned out. Other satisfactory natural crystal Carrier material made of an inorganic oxide gel line zeolites are, for example, analcite, paulingite, or clay and the compound mate- clinoptilatite, ferrierite, chabazite, gmelinite, levynite, rial, if necessary after washing, a further erionite and mordenite. Subjects ion exchange, dries and given- Among the most suitable synthetic crystalline aluminum cases at temperatures from 260 to 871 ° C with water minosilicates include the synthetic faujasites, and steam treated. both X and Y types, which one From BE-PS 6 12 551 a method for Her- crystal structure corresponding to that of natural position of a hydrocracking catalyst known to have with Lichem faujasite. The manufacture of such