JPS6257573B2 - - Google Patents

Description

[Detailed description of the invention]

The present invention relates to crystalline aluminosilicate zeolite compositions. More particularly, the present invention relates to crystalline zeolites that are crystallized in the presence of certain metals or metal compounds. The invention further relates to a hydrocarbon conversion catalyst comprising the same. In the past, zeolite materials have been shown to have catalytic ability in various types of hydrocarbon conversion reactions, both natural and synthetic.
Some zeolite materials are ordered, porous, crystalline aluminosilicates with a certain crystal structure, which contains many small pores that are divided into smaller channels. Therefore, they are interconnected. These holes and grooves have exactly uniform size. These pores adsorb and accept molecules of a certain standard size, but exclude larger molecules.
These materials are known as "molecular sieves" and are used in a variety of applications by taking advantage of these properties. Examples of these molecular sieves include various cation-containing crystalline aluminosilicates, both natural and synthetic. These aluminosilicates can be represented as rigid three-dimensional networks of SiO ₄ and AlO ₄ , whose tetrahedrons are cross-linked by sharing oxygen atoms, and whose total amount of aluminum and silicon atoms/ The ratio of oxygen atoms is 1/
It is 2. The electron valence of aluminum in the tetrahedron is balanced by incorporating cations such as alkali metals or alkaline earth metals into the crystal. This is Ca/2, Sr/2, Na, K
Alternatively, it can be expressed by the ratio of the number of various cations such as Li to Al being 1. One type of cation can be partially or totally exchanged for another type of cation by conventional ion exchange techniques. Such cation exchange has made it possible to change the pore size of certain aluminosilicates by appropriate selection of specific cations. The space between the tetrahedra is occupied by water molecules before dehydration. U.S. Pat. No. 3,941,871 describes and claims crystalline metal organosilicates with high silica/alumina ratios containing sodium, calcium, nickel or zinc. Other prior art describes the production of various synthetic crystalline aluminosilicates. These aluminosilicates are represented by letters or other convenient symbols, such as Zeolite A (U.S. Pat. No. 2,882,243), Zeolite X (U.S. Pat.
2882244), Zeolite ZSM-5 (U.S. Patent No.
3702886), Zeolite ZSM-11 (U.S. Patent No.
3709979), ZSM-12 (US Patent No. 3832449)
and zeolite ZSM-35 (US Patent No. 4016245
) etc. The present invention relates to a stable synthetic crystalline aluminosilicate zeolite composition, a method for making the same, and a method for converting hydrocarbons using the same. These synthesized compositions had a certain X-ray diffraction pattern as shown in Table 1 below, which is characteristic of ZSM-5 zeolite.

Table: These values were determined by standard methods.
The radiation was a copper K-alpha twin beam, and a self-recording scintillation counter spectrometer was used.
The peak height I and its position as a function of double θ (θ=Bragg angle) were read from the spectrometer chart. From these values, the relative intensity is 100I/Io
(Io is the strongest line, i.e. peak intensity),
And the lattice spacings A and d (observed values) corresponding to the recorded lines were calculated. It should be understood that this X-ray diffraction pattern is characteristic of all types of compositions of the present invention. Even when sodium ions are ion-exchanged with other cations, the lattice spacing shifts slightly and the relative intensity changes slightly, but essentially the same pattern is obtained. It may also vary slightly depending on the silicon/aluminum ratio and heat treatment conditions. Anhydrous compositions can also be expressed in terms of molar ratios of oxides as follows: [R ₂ O, M′〓O] w: [Al ₂ O ₃ ] x: [Sio ₂ ]
y: [M″〓O]z In the above formula, w/x=0.5~3, y/x=>20, z/
x=0-100, and R is a nitrogen-containing cation. R is a primary amine having 2 to 10 carbon atoms and an ammonium cation, preferably a tetraalkylammonium having an alkyl group having 2 to 5 carbon atoms, and M' is a metal of group 1A of the periodic table. , ammonium, hydrogen or a mixture thereof, where n is the valence of M′ or M″. In the case of M″, preferred metals are rare earth metals (i.e. metals with atomic numbers 57 to 71), chromium, vanadium, selected from molybdenum, indium, boron, mercury, tellurium, silver and platinum group metals (platinum, palladium and ruthenium). M'' may be present as a metal or as a metal compound. It is to be understood that the above formula may exist in various states and in varying amounts. For example, when present in the adsorbed state, the relative concentration to aluminum in synthetic zeolites is about 100 or less. tetrapropylammonium cation (e.g. derived from hydroxide), sodium oxide,
Silica, water and indium, boron, ruthenium, platinum, chromium, rare earths, vanadium, mercury,
Reaction mixtures containing tellurium, palladium, molybdenum or optional alumina sources produce ZSM-5 zeolites with unexpectedly improved properties. The amounts of indium, boron, etc. listed above are about 0.005-5.0% by weight of the final product. The crystalline aluminosilicate produced by the method of the present invention has high thermal stability and excellent catalytic properties. The alkali metals initially present can be at least partially exchanged for other cations using conventional ion exchange techniques. Examples of preferred exchange cations include metal ions, ammonium ions, hydrogen ions, and mixtures thereof. Particularly preferred cations are those which make the zeolite catalytically active (particularly in hydrocarbon conversion reactions).
Examples of these are hydrogen, metals of groups 1 and 2 of the periodic table, and manganese. Preferred zeolites have a silica/alumina ratio of 35
Larger, up to about 3000. The high thermal stability of the zeolite of the present invention makes it particularly useful for use in processes involving high temperature processing. The compositions of the present invention are manufactured using raw materials that provide the appropriate components of the zeolite. In the case of aluminosilicates, examples of such components are sodium aluminate, alumina, sodium silicate, silica hydrosol, silica gel, silicic acid, sodium hydroxide and tetrapropylammonium compounds (e.g. tetrapropylammonium hydroxide). . Each component used in the reaction mixture for producing zeolite is provided by one or more initial reactants, which may be mixed in any order. For example, sodium is supplied by an aqueous sodium hydroxide or sodium silicate solution, and the tetrapropylammonium cation is supplied by its bromide salt. The reaction mixture may be prepared in either a four-part or continuous manner. The crystal size and crystallization time of the composition will vary depending on the nature of the reaction mixture used. In the case of producing a product with a very high silica/alumina ratio of 35 to about 3000, preferably about 70 to about 500, as in the present invention, there is no need to add an alumina source to the reaction mixture; It is to be understood that the amount present is sufficient. The zeolites of the invention are prepared from reaction mixtures having a composition in the following ranges, expressed as molar ratios of oxides or expressed as % of total moles of oxides.

[Table] In the above table, R is the same as defined previously. Typical reaction conditions are to reduce the reaction mixture to about 95 to
It consists of heating to a temperature of 175°C for about 6 hours to 120 days. A more preferable temperature range is about 100-175℃
The heating time at this temperature range is approximately 12 hours to 8 days. Digestion of the gel particles is carried out until crystals form. The solid product obtained is separated from the reaction medium by cooling the whole to room temperature, filtering and washing with water. The product is, for example, at 110.0°C (230°C)
Allow to dry for ~24 hours. Naturally, drying may be carried out under milder conditions, for example, at room temperature under vacuum, if necessary. The zeolites of the present invention are capable of ion-exchanging the alkali metals bound thereto with a variety of other cations by conventional ion-exchange techniques. Examples of typical exchange cations include hydrogen, ammonium and metal cations, and mixtures thereof. Particularly preferred replacement metal cations include the rare earth metals, manganese and calcium, and the metals of Groups and Groups of the Periodic Table (eg, zinc or platinum). A typical ion exchange technique consists of contacting a zeolite with a salt of the desired exchange cation.
Various salts can be used for this purpose, but particularly preferred are the chlorides, nitrates and sulfates. For typical ion exchange technology, see US Patent No.
It is described in No. 3140249, No. 3140251, No. 3140253, etc. The zeolite is contacted with a solution of the salt of the desired exchange cation and then preferably washed with water, 65.6~
Dry at a temperature of about 315.6 °C (150 to about 600 °C) and then dry in air or other inert gas to about 260.0 °C
Bake at 815.6℃ (500-1500℃) for 1 minute to over 48 hours. Aluminum, silicon and oxygen form the basic crystal lattice of the zeolite as seen from the X-ray powder diffraction pattern of the ion-exchanged material, regardless of whether sodium or other alkali metals in the synthetic form are replaced with any other cation. The spatial arrangement of atoms remains essentially unchanged. Such X-ray diffraction patterns of the ion-exchanged products are substantially the same as those listed in Table 1 above. Aluminosilicates produced according to the present invention are formed into a variety of specific sizes. Generally, the resulting particles are in the form of extrudates, granules, or powders having a particle size that passes through a 2-mesh (Tyler mesh) sieve but not a 400-mesh (Tyler mesh) sieve. ing. When molding the catalyst by extrusion molding or the like, extrusion molding may be performed before drying, or after drying or partially drying. As is the case with many catalysts, it is desirable to incorporate into the zeolite durable materials that withstand the temperatures and other conditions used in organic conversion processes. Examples of these durable substances include active and inert substances;
There are synthetic or natural zeolites as well as inorganic materials such as clays, silicas and/or metal oxides.
The latter may be natural or in the form of a gelatinous precipitate or gel and contain a mixture of silica and metal oxides. When active materials are combined in the compositions of the present invention, they tend to improve the conversion and/or selectivity of catalysts in certain organic conversion processes. Inert substances suitably act as diluents to control the amount of conversion in certain processes, so that products can be obtained in an economical and orderly manner, especially without the use of other means to control the reaction rate. . Zeolitic materials are typically mixed with naturally occurring clays such as bentonite and kaolin to improve the crush strength of the catalyst under commercial operating conditions. clay,
These substances, such as oxides, act as binders for the catalyst. It is desirable to provide a catalyst with good crush strength since in petroleum refining processes catalysts are often handled roughly and tend to break down into powder, creating problems during operation. These clay binders were used for the purpose of improving the crush strength of the catalyst. Examples of natural clays that are composited with catalysts include montmorillonite and kaolins, which include subbentonite and kaolin, which are commonly known as Dixie, McNamee, Georgea, and Florida clays, and whose main minerals are The ingredients are halloysite, kaolinite, dateskite, nacrite, or anorchisite. These clays may be used in their raw state as they are mined, but they may also be first calcined, acid-treated, or chemically modified. In addition to the above-mentioned materials, the catalyst may be composited with porous host materials, examples of which include silica, alumina, silica-alumina, silica-magnesia, silica-zirconia, silica-thoria,
Examples include silica-beryria, silica-titania, and ternary systems such as silica-alumina-thoria, silica-alumina-zirconia, silica-alumina-magnesia, and silica-magnesia-zirconia. This matrix may be in the form of a co-gel. The relative proportions of the finely divided crystalline aluminosilicate and the inorganic oxide gel matrix vary over a wide range, with the crystalline aluminosilicate content ranging from about 1 to about 1% of the composite.
90% by weight, and from about 2 to about 50% by weight, particularly when the composite is made in the form of beads. The catalysts of the present invention are useful in cracking and hydrocracking, as well as in other petroleum refining processes, and exhibit unique catalytic properties. Examples of the latter reactions for which the catalyst of the present invention is effective include isomerization reactions of n-paraffin and naphthene, polymerization reactions of compounds having olefinic or acetylenic carbon-carbon bonds such as isobutylene and butene-1, and reforming reactions. , alkylation reactions, isomerization reactions of polyalkyl-substituted aromatics such as ortho-xylene, and disproportionation reactions of aromatics such as toluene to provide mixtures of benzene, xylene and methylbenzene. The catalyst of the present invention is highly selective compared to previously known zeolite catalysts for hydrocarbon conversion and provides large amounts of the desired product under hydrocarbon conversion conditions. The zeolites of the present invention are also useful in other catalytic processes, such as catalytic cracking and hydrocracking of hydrocarbons. Under these conditions, this type of zeolite not only has high thermal stability, but also serves to convert cracked oils into lower boiling point, lower molecular weight materials that are more economically valuable. The property of being physically stable at high temperatures and/or in the presence of high temperature steam is very important as a cracking catalyst. During the catalytic conversion process, the reaction that occurs is essentially cracking to produce hydrocarbons. However, this cracking involves several complicated side reactions such as aromatization, polymerization, and alkylation reactions. As a result of these complex reactions, carbonaceous deposits called "coke" are deposited on the catalyst. Coke deposited on the catalyst significantly reduces the catalytic efficiency of the desired main surface reaction and substantially reduces the conversion rate and/or selectivity. It is therefore common to remove the catalyst after the coke has been deposited and regenerate it by burning the coke in a stream of oxidizing gas. The regenerated catalyst is returned to the conversion stage of the process. In this respect, the high thermal stability of zeolites is advantageous. The catalyst product may be used in any form: alkali metal such as sodium, ammonium, hydrogen or other monovalent or polyvalent cations. Preferably either of the latter two forms is used. The catalyst composition can be used in combination with hydrogenation components such as tungsten, vanadium, molybdenum, rhenium, nickel, cobalt, chromium, manganese or noble metals (e.g. platinum or palladium) when carrying out hydrogenation/dehydrogenation reactions. May be used. These components can be incorporated into the catalyst composition by ion exchange, impregnation, or intimate physical mixing. These components can be impregnated, for example in the case of platinum, by treating the zeolite with platinum-containing ions. Examples of suitable platinum compounds include dichloroplatinic acid, platinous chloride, and various compounds containing platinum-amine complexes. Useful compounds of platinum or other metals are divided into those in which the metal is present as a cation and those in which the metal is present as an anion. Both types of compounds containing metals in ionic form can be used. Particularly useful are solutions in which the platinum is in the form of a cation or cationic complex, such as Pt(NH ₃ ) ₆ Cl ₄ . For certain hydrocarbon conversion reactions, such as low temperature liquid phase ortho-xylene isomerization reactions, such noble metal forms of catalyst are unnecessary. When used as either an adsorbent or a catalyst in any of the above reactions, the catalyst must be at least partially dehydrated. This is accomplished by heating at a temperature of 200 to 600° C. for 1 minute to 48 hours at atmospheric pressure or subatmospheric pressure in an atmosphere of air, nitrogen, or the like. Dehydration can also be achieved by simply placing the catalyst under vacuum at a lower temperature, but longer times are required to achieve sufficient dehydration. The invention will be further illustrated by the following examples. Example 1 Solution 1 Q brand silicate 240g Distilled H ₂ O 300g Total 540g Solution 2 Distilled H ₂ O 410g Tetrapropylammonium bromide 30g Concentrated sulfuric acid 20g crK (SO ₄ ) ₂・12H ₂ O 12.25g Q brand is Philadelphia Quartz Co.'s brand of sodium silicate, and the typical analysis value is
Na ₂ O = 8.9%, SiO ₂ = 28.7%, H ₂ O = 62.4%. Solution 1 was placed in a 4-neck, 2-fill flask equipped with a stirrer. Solution 2 was added with stirring. This solution became very gelatinous. a small amount of H-
ZSM-5 (approximately 1.0 g) was added as a crystal nucleus. Heating was started and the solution was heated to approximately 96.1°C (205°C). A variable voltage transformer suppressed the temperature to ±3°C/day according to voltage changes. After a few days, the solution lost its gelatinous character and became more yolk-like. Crystallization took 5-6 days as determined by X-ray. The resulting catalyst was filtered and washed with approximately 4 portions of distilled _H2O . This gave 60-70 g of catalyst. The catalyst was dried at 70°C, placed in a crucible, and calcined in a Matsufuru furnace at 239-537.8°C (75-1000°C) for 12 hours. This catalyst was mixed with 100 c.c. of H ₂ O and 10 g of
Pour into a _200ml flask with _NH4NO3 ,
The mixture was refluxed at 100°C for 1 hour. The catalyst was filtered, washed and ion exchanged with NH ₄ NO ₃ for 5 hours. The catalyst was filtered again, washed and the ion exchange was repeated for about 16 hours. The catalyst was filtered, washed thoroughly and dried at 70°C for about 6 hours. This catalyst was heated again in the Matsufuru furnace at 23.9~537.8℃ (75~1000℃).
〓) for 6 hours. The X-ray powder diffraction patterns of this crystalline product as synthesized and after the treatment as described above were measured, and the results are shown in Table 3. Although the example here uses ammonium cations, other cations such as alkylammonium, metals, and hydrogen may also be used. As can be seen from Table 3, minute differences are observed in the X-ray diffraction patterns of the as-synthesized zeolite and the zeolite after ion exchange and heat treatment. These differences are changes from single lines to doublets and other doublets to single lines caused by minute shifts in lattice spacing and changes in relative intensity. These differences are reflected in minute changes in lattice parameters and crystal symmetry.

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TABLE The X-ray diffraction patterns of the catalysts for each material in the examples below (ie, Examples 2-8) are shown in the table following the examples. Example 2 5g of chromium compound and sulfuric acid
Prepared as in Example 1 except that RuCI _{2.3H 2} O and 35 g of HCl were used. The X-ray diffraction pattern of this material is shown in Table 1.
Substantially all characteristic lines of ZSM-5 zeolite are shown. As in the case of the first example, when the zeolites of this example and the six examples below are subjected to ion exchange, thermal conditioning, or other treatments, similar small changes in lattice spacing, lattice symmetry, and relative strength occur. occurred.

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[Table] Example 3 2g of H ₂ PtCl ₆・nH ₂ O instead of chromium compound
It was produced in the same manner as in Example 1 except that .

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[Table] Example 4 6.3g of In ₂ instead of chromium potassium sulfate
It was produced in the same manner as in Example 1 except that (SO ₄ ) ₃ was used.

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[Table] Example 5 A product was produced in the same manner as in Example 1 except that 5.8 g of Ce(SO ₄ ) ₂ and 3.7 g of Al ₂ (SO ₄ ) _{3.14H 2} O were used instead of the chromium compound.

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[Table] Example 6 A product was prepared in the same manner as in Example 1, except that 223 g of V ₂ O ₅ was used instead of the chromium compound.

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[Table] Example 7 Example 1 except that 1.5 g of Zn ₂ B ₆ O ₁₁ and 25 g of tetraethylammonium bromide were used instead of the chromium compound and tetrapropylammonium bromide.
Manufactured in the same way.

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[Table] Example 8 A product was produced in the same manner as in Example 1, except that 397 g of molybdic acid (H ₂ M ₀ O ₄ ) was used instead of the chromium compound.

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[Table] Example 9 Produced in the same manner as in Example 1 except that 5 g of silver acetate was used instead of the chromium compound. The results of the X-ray analysis were found to have a similar pattern to the previous example. Example 10 Produced as in Example 1 except that 35 g of HCl was used instead of sulfuric acid and 5 g of HgCl ₂ was used instead of the chromium compound. The results of the X-ray analysis were found to have a similar pattern to the previous example. Example 11 Produced as in Example 1 except that 5 g of H ₆ TeO ₆ was used instead of the chromium compound. The results of X-ray analysis were found to have a similar pattern as above. When using the catalyst of the present invention containing a hydrogenation component, heavy petroleum residue, recirculation at a hydrogen/hydrocarbon feedstock molar ratio of 2 to 80 and a temperature of 204.4 to 440.5°C (400 to 825〓) is used. Oils and other hydrocrackable raw materials can be hydrocracked.
The pressure used is 0.7~176Kg/cm ² gauge pressure (10~
2500psig) and the liquid hourly space velocity is 0.1~10
It is. When using the catalyst of the present invention for catalytic cracking, the hydrocarbon cracking feedstock is about 0.5 to
At a liquid hourly space velocity of 50, 287.8~593.3℃ (500
Cracking is possible at temperatures ranging from ~1100〓) and pressures ranging from below atmospheric pressure to several hundred atmospheres. When using the catalytically active form of the zeolite of the present invention containing a hydrogenated component, the reforming feedstock can be reformed using temperatures between 700 and 1000°C. In this case, the pressure is 7.0~70.3Kg/ ^cm2 gauge pressure (100~
1000psig), preferably 14.1-49.2Kg/ ^cm2 gauge pressure (200-700psig), and the liquid hourly space velocity is
The hydrogen/hydrocarbon molar ratio is generally between 1 and 20, preferably between 4 and 12. The catalyst of the present invention can also be used to hydroisomerize n-paraffins when equipped with a hydrogenation component (eg platinum). The hydroisomerization reaction is
93.3~37.1℃ (200~700〓), preferably 148.9~
It is carried out at a temperature of 300 to 550 °C, a liquid hourly space velocity of 0.01 to 2, preferably 0.25 to 0.50, and a hydrogen/hydrocarbon molar ratio of 1/1 to 5/1. Furthermore, the catalyst of the present invention is -1.1~260.0℃ (30~260.0℃)
It can also be used for the isomerization reaction of olefins at a temperature of 500㎓), and can also be used for the conversion reaction of methanol and dimethyl ether. Examples of other reactions that can be carried out using the catalysts of the invention containing metals such as platinum include hydrogenation-dehydrogenation reactions, desulfurization reactions, and hydrocarbon oxidation reactions. The catalyst products of the present invention were tested in several of the conversion reactions described above, and the results are shown below. Catalyst Product Evaluation Toluene Disproportionation Reaction Table 11 summarizes the data obtained on toluene conversion using various samples of hydrogenated zeolite. The operation was carried out at 42.2 Kg/cm ² gauge pressure (600 psig), WHSV = 3.5, hydrogen/hydrocarbon (H ₂ /HC) molar ratio = 2/1, and other conditions are shown in Table 11. It was obtained by the procedure of Example 1 for the hydrogen type catalyst.

[Table] Hydrocracking reaction Table 12 shows 106.7~
185.0℃ (224~365〓)
The results are shown for conversion at temperatures of 482.2-537.8°C (900-1000〓). Conversion was carried out at 7.0 Kg/cm ² gauge pressure (100 psig) with WHSV=5 and H ₂ /HC=3/1. This naphtha had the properties shown in the table below. The hydrogen type zeolite was obtained as described above.

[Table] Reaction of methanol Vaporized methanol was passed over hydrogen-type zeolite manufactured using platinum. The reaction conditions and results are shown in Table 13.

[Table] Xylene isomerization reaction The same zeolites used in the tests listed in Table 13 were tested for their activity in the xylene isomerization reaction. Table 14 shows the reaction conditions and results.

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Table: The feeds listed in Table 15 were passed over the same catalysts used in Tables 13 and 14. The reaction conditions and the results obtained are shown in Table 15.

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Claims (1)

[Scope of Claims] 1 The following formula expressed as the molar ratio of oxides in an anhydrous state: [R ₂ O, M′〓O] w: [Al ₂ O ₃ ] x: [SiO ₂ ]
y: [M″〓O]z (in the above formula w/x=0.5~3, y/x=>20,
z/x=0 to 100, R is a nitrogen-containing cation, M′ is a metal of Group A of the periodic table, M″ is indium, boron, ruthenium, platinum, chromium, rare earth, vanadium, palladium,
a metal selected from the group consisting of molybdenum, mercury, tellurium, silver and mixtures of these metals,
n is the valence of the metal) and having an X-ray diffraction pattern substantially as set forth in Table 1 of the specification. 2. The zeolite composition according to claim 1, wherein R is a tetraalkylammonium cation having an alkyl group having 2 to 5 carbon atoms. 3 R and/or M' are alkylammonium,
The zeolite composition according to claim 1, which is substituted with a cation selected from the group consisting of metal, ammonium, hydrogen and mixtures thereof. 4. The zeolite composition according to claim 3, wherein the zeolite composition is heat-treated at a temperature higher than 260.0°C (500°C). 5 Claim 1 in which M' is sodium
The zeolite composition described in . The zeolite composition of claim 1, wherein 6 M'' is selected from the group consisting of chromium, ruthenium, platinum, indium, cerium, vanadium, boron, molybdenum, mercury, tellurium and silver. 7 M 7. The zeolite composition according to claim 6, wherein `` is chromium. Claim 6 in which 8 M″ is ruthenium
The zeolite composition described in . The zeolite composition of claim 6, wherein 9 M'' is platinum. The zeolite composition of claim 6, wherein 10 M'' is indium. Claim 6 in which 11 M″ is cerium
Compositions as described in Section. The zeolite composition of claim 6, wherein 12 M'' is vanadium. The zeolite composition of claim 6, wherein 13 M'' is boron. 7. The zeolite composition of claim 6, wherein 14 M" is molybdenum. The zeolite composition of claim 6, wherein 15 M" is mercury. The zeolite composition of claim 6, wherein 16 M'' is tellurium. The zeolite composition of claim 6, wherein 17 M'' is silver. 18. The zeolite composition according to claim 1, having a SiO ₂ /Al ₂ O ₃ ratio of 35 to 3000. 19 Expressed as the molar ratio of oxides in an anhydrous state, the following formula: [R ₂ O, M′〓O] w: [Al ₂ O ₃ ] x: [SiO ₂ ]
y: [M″〓O]z (in the above formula w/x=0.5~3, y/z=>20,
z/x=0 to 100, R is a nitrogen-containing cation, M′ is a metal of Group A of the periodic table, M″ is indium, boron, ruthenium, platinum, chromium, rare earth, vanadium, palladium,
a metal selected from the group consisting of molybdenum, mercury, tellurium, silver and mixtures of these metals,
n is the valence of the metal) and having an X-ray diffraction pattern substantially as described in Table 1 of the specification, characterized in that the organic feedstock is passed under conversion conditions over a crystalline aluminosilicate zeolite composition having an X-ray diffraction pattern substantially as described in Table 1 of the specification. Catalyst for conversion of organic raw materials. 20. The conversion catalyst according to claim 19, which uses a zeolite composition in which 20R is a tetraalkylammonium cation having an alkyl group having 2 to 5 carbon atoms. 21. The conversion catalyst according to claim 19, which uses a thermally treated zeolite composition. 22 Zeolite compositions in which R and/or M' are substituted with cations selected from the group consisting of alkylammonium, metals, ammonium, hydrogen and mixtures thereof, and which have been heat treated at a temperature higher than 260.0°C (5000〓) 20. The conversion catalyst according to claim 19, which uses a catalyst. 23. The conversion catalyst according to claim 19, which uses a zeolite composition in which 23 M' is sodium. 24 M'' is selected from the group consisting of chromium, ruthenium, platinum, indium, cerium, vanadium, boron, molybdenum, mercury, tellurium and silver. Conversion Catalyst. The conversion catalyst of claim 24 using a zeolite composition in which 25 M'' is chromium. The conversion catalyst according to claim 24, which uses a zeolite composition in which 26 M'' is ruthenium. The conversion catalyst according to claim 24, which uses a zeolite composition in which 27 M'' is platinum. The conversion catalyst according to claim 24, which uses a zeolite composition in which 28 M'' is indium. The conversion catalyst according to claim 24, which uses a zeolite composition in which 29 M'' is cerium. 25. The conversion catalyst of claim 24 using a zeolite composition in which 30 M" is vanadium. The conversion catalyst of claim 24 using a zeolite composition in which 31 M" is boron. The conversion catalyst according to claim 24, which uses a zeolite composition in which 32 M'' is molybdenum. The conversion catalyst according to claim 24, which uses a zeolite composition in which 33 M'' is mercury. 25. The conversion catalyst of claim 24 using a zeolite composition in which 34 M'' is tellurium. The conversion catalyst of claim 24 using a zeolite composition in which 35 M'' is silver. 36. The conversion catalyst according to claim 19, which uses a zeolite composition having a SiO ₂ /Al ₂ O ₃ ratio of 35 to 3000.