USRE29857E - Conversion with ZSM-5 family of crystalline aluminosilicate zeolites - Google Patents
Conversion with ZSM-5 family of crystalline aluminosilicate zeolites Download PDFInfo
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- USRE29857E USRE29857E US05/866,576 US86657678A USRE29857E US RE29857 E USRE29857 E US RE29857E US 86657678 A US86657678 A US 86657678A US RE29857 E USRE29857 E US RE29857E
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
- C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
- C10G47/12—Inorganic carriers
- C10G47/16—Crystalline alumino-silicate carriers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/20—Silicates
- C01B33/26—Aluminium-containing silicates, i.e. silico-aluminates
- C01B33/28—Base exchange silicates, e.g. zeolites
- C01B33/2807—Zeolitic silicoaluminates with a tridimensional crystalline structure possessing molecular sieve properties; Isomorphous compounds wherein a part of the aluminium ore of the silicon present may be replaced by other elements such as gallium, germanium, phosphorus; Preparation of zeolitic molecular sieves from molecular sieves of another type or from preformed reacting mixtures
- C01B33/2884—Zeolitic silicoaluminates with a tridimensional crystalline structure possessing molecular sieve properties; Isomorphous compounds wherein a part of the aluminium ore of the silicon present may be replaced by other elements such as gallium, germanium, phosphorus; Preparation of zeolitic molecular sieves from molecular sieves of another type or from preformed reacting mixtures the aluminium or the silicon in the network being partly replaced
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B39/00—Compounds having molecular sieve and base-exchange properties, e.g. crystalline zeolites; Their preparation; After-treatment, e.g. ion-exchange or dealumination
- C01B39/02—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof; Direct preparation thereof; Preparation thereof starting from a reaction mixture containing a crystalline zeolite of another type, or from preformed reactants; After-treatment thereof
- C01B39/36—Pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
- C01B39/38—Type ZSM-5
- C01B39/40—Type ZSM-5 using at least one organic template directing agent
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
- C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C6/00—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions
- C07C6/08—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond
- C07C6/12—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring
- C07C6/123—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions by conversion at a saturated carbon-to-carbon bond of exclusively hydrocarbons containing a six-membered aromatic ring of only one hydrocarbon
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
- C10G11/04—Oxides
- C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G35/00—Reforming naphtha
- C10G35/04—Catalytic reforming
- C10G35/06—Catalytic reforming characterised by the catalyst used
- C10G35/095—Catalytic reforming characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
- C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
- C10G45/64—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/30—After treatment, characterised by the means used
- B01J2229/40—Special temperature treatment, i.e. other than just for template removal
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
Definitions
- This invention relates to novel crystalline aluminosilicates and to methods for the preparation. More particularly, this invention relates to novel crystalline alumino-silicates having catalytic properties, to methods for preparing the same, and hydrocarbon conversion therewith.
- Zeolitic materials both natural and synthetic, have been demonstrated in the past to have catalytic capabilities for various types of hydrocarbon conversion.
- Certain zeolithic materials are ordered porous crystalline aluminosilicates having a definite crystalline structure within which there are a large number of small cavities which are interconnected by a number of still smaller channels. These cavities and channels are precisely uniform in size. Since the dimensions of these pores are such as to accept for adsorption molecules of certain dimensions while rejecting those of larger dimensions, these materials have come to be known as "molecular sieves" and are utilized in a variety of ways to take advantage of these properties.
- Such molecular sieves include a wide variety of positive ion-containing crystalline aluminosilicates, both natural and synthetic. These aluminosilicates can be described as a rigid three-dimensional network of SiO 4 and and AlO 4 in which the tetrahedra are cross-linked by the sharing of oxygen atoms whereby the ratio of the total aluminum and silicon atoms to oxygen is 1:2.
- the electrovalence of the tetrahedra-containing aluminum is balanced by the inclusion in the crystal of a cation, for example, an alkali metal or an alkaline earth metal cation.
- zeolite A U.S. 2,882,243
- zeolite X U.S. 2,882,244
- zeolite Y U.S. 3,130,007
- zeolite K-G U.S. 3,055,654
- zeolite ZK-5 U.S. 3,247,195
- zeolite Beta U.S. 3,308,069
- zeolite ZK-4 U.S. 3,314,752
- the present invention relates to a novel family of ultrastable synthetic siliceous crystalline materials, hereinafter designated as "Zeolite ZSM-5" or simply “ZSM-5" to methods for the preparation and to hydrocarbon conversion processes conducted therewith.
- the family of ZSM-5 comositions has the characteristic X-ray diffraction pattern set forth in Table 1, hereinbelow.
- ZSM-5 a compositions can also be identified, in terms of mole ratios of oxides, as follows:
- the zeolite has a formula, in terms of mole ratios of oxides, as follows:
- M is selected from the group consisting of a mixture of alkali metal cations, especially sodium, and tetraalkylammonium cations, the alkyl groups of which preferably contains 2-5 carbon atoms.
- the original cations can be replaced in accordance with techniques well-known in the art, at least in part, by ion exchange with other cations.
- Preferred replacing cations include tetraalkylammonium cations, metal ions, ammonium ions, hydrogen ions, and mixtures of the same.
- Particularly preferred cations are those which render the zeolite catalytically active, especially for hydrocarbon conversion. These include hydrogen, rare earth metals, aluminum, metals of Groups II and VIII of the Periodic Table and manganese.
- W is aluminum
- Y is silicon
- the silica/alumina mole ratio is at least 10 and ranges up to about 60.
- ZSM-5 Members of the family of zeolites designated herein as ZSM-5 have an exceptionally high degree of thermal stability thereby rendering them particularly effective for use in processes involving elevated temperatures.
- ZSM-5 zeolites appear to be one of the most stable families of zeolites known to date.
- the radiation was the K-alpha doublet of copper, and a scintillation counter spectrometer with a strip chart pen recorder was used.
- this X-ray diffraction pattern is characteristic of all the species of ZSM-5 compositions. Ion exchange of the sodium ion with cations reveals substantially the same pattern with some minor shifts in interplanar spacing and variation in relative intensity. Other minor variations can occur depending on the silicon to aluminum ratio of the particular sample, as well as if it has been subjected to thermal treatment. Various cation exchanged forms of ZSM-5 have been prepared. X-ray powder diffraction patterns of several of these forms are set forth below. The ZSM-5 forms set forth below are all aluminosilicates.
- ZSM-5 zeolites are useful in cracking and hydrocracking, they are outstandingly useful in other petroleum refining processes indicating again the unique catalytic characteristics of this family of zeolites.
- the later processes include isomerization of n-paraffins and naphthenes, polymerization of compounds containing an olefinic or acetylinic carbon to carbon linkage such as isobutylene and butene-1, reforming, alkylation, isomerization of polyalkyl substituted aromatics, e.g., ortho xylene and disproportionation of aromatics, such as toluene to provide a mixture of benzene, xylenes and higher methylbenzenes.
- the ZSM-5 catalysts have exceptional high selectivity and under the conditions of hydrocarbon conversion provide a high percentage of desired products relative to total products compared with known zeolitic hydrocarbon conversion catalysts.
- ZSM-5 zeolites are also useful in other catalytic processes, such as catalytic cracking of hydrocarbons and hydrocracking.
- catalytic cracking of hydrocarbons and hydrocracking In addition to the thermal stability of this family of zeolites under these conditions, they provide conversion of the cracked oil to materials having lower molecular weights and boiling points which are of greater economic value.
- the ability to be physically stable under high temperatures and/or in the presence of high temperature steam is extremely important for a cracking catalyst.
- the reaction which takes place is essentially a cracking to produce hydrocarbons.
- this cracking is accompanied by a number of complex side reactions such as aromatization, polymerization, alkylation and the like.
- ZSM-5 zeolites can be used either in the alkali metal form, e.g., the sodium form, the ammonium form, the hydrogen form, or another univalent or multivalent cationic form. Preferably, one or other of the last two forms is employed. They can also be used in intimate combination with a hydrogenating component such as tungsten, vanadium, molybdenum, rhenium, nickel, cobalt, chromium, manganese, or a noble metal such as platinum or palladium where a hydrogenation dehydrogenation function is to be performed. Such component can be exchanged into the composition, impregnated therein or physically intimately admixed therewith.
- a hydrogenating component such as tungsten, vanadium, molybdenum, rhenium, nickel, cobalt, chromium, manganese, or a noble metal such as platinum or palladium where a hydrogenation dehydrogenation function is to be performed.
- a hydrogenating component such as tungsten
- Such component can be impregnated in or on to ZSM-5 such as, for example, by, in the case of platinum, treating the zeolite with a platinum metal-containing ion.
- suitable platinum compounds include chloroplatinic acid, platinous chloride and various compounds containing the platinum ammine complex.
- the compounds of the useful platinum or other metals can be divided into compounds in which the metal is present in the cation of the compound and compounds in which it is present in the anion of the compound. Both types of compounds which contain the metal in the ionic state can be used.
- this noble metal form of the ZSM-5 catalyst is unnecessary such as in low temperature, liquid phase ortho xylene isomerization.
- ZSM-5 when employed either as an adsorbent or as a catalyst in one of the aforementioned processes, should be dehydrated at least partially. This can be done by heating to a temperature in the range of 200 to 600° C. in an atmosphere such as air, nitrogen, etc. and at atmospheric or subatmospheric pressures for between 1 and 48 hours. Dehydration can aso be performed at lower temperatures merely by placing the ZSM-5 catalyst in a vacuum, but a longer time is required to obtain a sufficient amount of dehydration.
- Zeolite ZSM-5 can be suitably prepared by preparing a solution containing tetrapropyl ammonium hydroxide, sodium oxide, an oxide of aluminum or gallium, an oxide or silica or germanium, and water and having a composition, in terms of mole ratios of oxides, falling within the following ranges:
- R is propyl
- W is aluminum or gallium
- Y is silicon or germanium maintaining the mixture until crystals of the zeolite are formed.
- an excess of tetrapropylammonium hydroxide can be used which would raise the value of OH-/YO 2 above the ranges set forth supra. The excess hydroxide, of course, does not participate in the reaction. Thereafter, the crystals are separated from the liquid and recovered.
- Typical reaction conditions consist of heating the foregoing reaction mixture to a temperature of from about 100° C. to 175° C. for a period of time of from about six hours to 60 days. A more preferred temperature range is from about 150° to 175° C. with the amount of time at a temperature in such range being from about 12 hours to 8 days.
- the digestion of the gel particles is carried out until crystals form.
- the solid product is separated from the reaction medium, as by cooling the whole to room temperature, filtering, and water washing.
- the foregoing product is dried, e.g., at 230° F., for from about 8 to 24 hours.
- milder conditions may be employed if desired, e.g., room temperature under vacuum.
- ZSM-5 is preferably formed as an aluminosilicate.
- the composition can be prepared utilizing materials which supply the appropriate oxide.
- Such compositions include for an aluminosilicate, sodium aluminate, alumina, sodium silicate, silica hydrosol, silica gel, silicic acid, sodium hydroxide and tetrapropylammonium compounds, e.g., tetrapropylammonium hydroxide.
- each oxide component utilized in the reaction mixture for preparing a member of the ZSM-5 family can be supplied by one of more initial reactants and they can be mixed together in any order.
- sodium oxide can be supplied by an aqueous solution of sodium hydroxide, or by an aqueous solution of sodium silicate; tetrapropylammonium cation can be supplied by the bromide salt.
- the reaction mixture can be prepared either batchwise or continuously. Crystal size and crystallization time of the ZSM-5 composition will vary with the nature of the reaction mixture employed.
- ZSM-5 family can have the original cations associated therewith replaced by a wide variety of other cations according to techniques well known in the art.
- Typical replacing cations would include hydrogen, ammonium and metal cations including mixtures of the same.
- replacing metallic cations particular preference is given to cations of metals such as rare earth metals, manganese, calcium, as well as metals of Group II of the Periodic Table, e.g., zinc, and Group VIII of the Periodic Table, e.g., nickel.
- Typical ion exchange techniques would be to contact the members of the family of ZSM-5 zeolites with a salt of the desired replacing cation or cations.
- a wide variety of salts can be employed, particular preference is given to chlorides, nitrates and sulfates.
- the zeolites are then preferably washed with water and dried at a temperature ranging from 150° F. to about 600° F. and thereafter calcined in air or other inert gas at temperatures ranging from about 500° F. to 1500° F. for periods of time ranging from 1 to 48 hours or more.
- the aluminosilicates prepared by the instant invention are formed in a wide variety of particular sizes.
- the particles can be in the form of a powder, a granule, or a molded product, such as extrudate having particle size sufficient to pass through a 2 mesh (Tyler) screen and be retained on a 400 mesh (Tyler) screen.
- the aluminosilicate can be extruded before drying or dried or partially dried and then extruded.
- the ZSM-5 in the case of many catalysts, it is desired to incorporate the ZSM-5 with another material resistant to the temperatures and other conditions employed in organic conversion processes.
- materials include active and inactive materials and synthetic or naturally occurring zeolites as well as inorganic materials such as clays, silica and/or metal oxides. The latter may be either naturally occurring or in the form of gelatinous precipitates or gels including mixtures of silica and metal oxides.
- Use of a material in conjunction with the ZSM-5, i.e., combined therewith which is active, tends to improve the conversion and/or selectivity of the catalyst in certain organic conversion processes.
- Inactive materials suitably serve as diluents to control the amount of conversion in a given process so that products can be obtained economically and orderly without employing other means for controlling the rate of reaction.
- zeolite materials have been incorporated into naturally occurring clays, e.g., bentonite and kaolin, to improve the crush strength of the catalyst under commercial operating conditions. These materials, i.e., clays, oxides, etc., function as binders for the catalyst. It is desirable to provide a catalyst having good crush strength, because in a petroleum refinery the catalyst is often subjected to rough handling, which tends to break the catalyst down into powder-like materials which cause problems in processing. These clay binders have been employed for the purpose of improving the crush strength of the catalyst.
- Naturally occurring clays which can be composited with the ZSM-5 catalyst include the montmorillonite and kaolin family, which families include the sub-bentonites, and the kaolins commonly known as Dixie McNamee-Georgia and Florida clays or others in which the main mineral constituent is halloysite, kaolinite, dickite, nacrite, or anauxite.
- Such clays can be used in the raw state as originally mined or initially subjected to calcination, acid treatment or chemical modification.
- the ZSM-5 catalyst can be composited with a porous matrix material such as silica-alumina, silica-magnesia, silica-zirconia, silica-thoria, silica-beryllia, silica-titania as well as ternary compositions such as silica-alumina-thoria, silica-alumina-zirconia, silica-alumina-magnesia and silica-magnesia-zirconia.
- the matrix can be in the form of a cogel.
- the relative proportions of finely divided crystalline alumino-silicate ZSM-5 and inorganic oxide gel matrix vary widely with the crystalline aluminosilicate content ranging from about 1 to about 90 percent by weight and more usually, particularly when the composite is prepared in the form of beads in the range of about 2 to about 50 percent by weight of the composite.
- ZSM-5 catalyst of this invention containing a hydrogenation component, heavy petroleum residual stocks, cyclic stocks, and other hydrocrackable charge stocks can be hydrocracked at temperatures between 400° F. and 825° F. using molar ratios of hydrogen to hydrocarbon charge in the range between 2 and 80.
- the pressure employed will vary between 10 and 2,500 p.s.i.g. and the liquid hourly space velocity between 0.1 and 10.
- Employing the catalyst of this invention for catalytic cracking hydrocarbon cracking stocks can be cracked at a liquid hourly space velocity between about 0.5 and 50, a temperature between about 550° F. and 1100° F., a pressure between about subatmospheric and several hundred atmospheres.
- reforming stocks can be reformed employing a temperature between 700° F. and 1000° F.
- the pressure can be between 100 and 1000 p.s.i.g. but is preferably between 200 and 700 p.s.i.g.
- the liquid hourly space velocity is generally between 0.1 and 10, preferably between 0.5 and 4 and the hydrogen to hydrocarbon mole ratio is generally between 1 and 20 preferably between 4 and 12.
- the catalyst can also be used for hydroisomerization of normal paraffins, when provided with a hydrogenation component, e.g., platinum. Hydroisomerization is carried out at a temperature between 200 and 700° F., preferably 300 to 550° F., with a liquid hourly space velocity between 0.01 and 2, preferably between 0.25 and 0.50 employing hydrogen such that the hydrogen to hydrocarbon mole ratio is between 1:1 and 5:1. Additionally, the catalyst can be used for olefin isomerization employing temperatures between 30° F. and 500° F.
- a weighed sample of the zeolite was contacted with the desired pure adsorbate vapor in an adsorption chamber at a pressure less than the vapor-liquid equilibrium pressure of the adsorbate at room temperature. This pressure was kept constant during the adsorption period which did not exceed about eight hours. Adsorption was complete when a constant pressure in the adsorption chamber was reached, i.e., 12 mm. of mercury for water and 20 mm. for n-hexane and cyclohexane. The increase in weight was calculated as the adsorption capacity of the sample.
- This example illustrates the preparation of zeolite ZSM-5.
- SiO 2 was partially dissolved in 100 ml. 2.18 N tetrapropylammonium hydroxide by heating to a temperature of about 100° C.
- NaAlO 2 comp: 42.0 wt. percent Al 2 O 3 , 30.9 wt. percent Na 2 O, 27.1 wt. percent H 2 O
- 53.8 ml. H 2 O 3
- the resultant mixture had the following composition: 0.382 mole SiO 2 , 0.0131 mole Al 2 O 3 , 0.0159 mole Na 2 O, 0.118 mole [(CH 3 CH 2 CH 2 ) 4 N] 2 O, 6.30 moles H 2 O.
- the mixture was placed in a Pyrex lined autoclave and heated at 150° C. for six days.
- the resultant solid product was cooled to room temperature, removed, filtered, washed with 1 liter H 2 O and dried at 230° F. A portion of this product was subjected to X-ray analysis and identified as ZSM-5. A portion of the product was calcined at 1000° F. in air for 16 hours and the following analyses were obtained:
- This example illustrates another preparation of Zeolite ZSM-5.
- 22.9 grams of SiO 2 were partially dissolved in 85.5 ml. of 2.21 N (CH 3 CH 2 CH 2 ) 4 NOH by heating to a temperature of about 100° C.
- the resultant mixture had the following composition: 0.382 mole SiO 2 , 0.0138 mole Al 2 O 3 , 0.0139 mole Na 2 O, 0.236 mole (CH 3 CH 2 CH 2 ) 4 NOH, and 6.25 moles H 2 O.
- This composition was placed in a Pyrex lined autoclave, heated to 150° C., and maintained at this temperature for five days.
- the resultant solid product was cooled to room temperature, removed, filtered and washed with 1 liter of water.
- the product was both grainy and dilatant. Microscopic examination showed the presence of very small crystals (on the order of 1 micron) along with some gel particles.
- the product was then calcined at 1000° F. The analysis of this product is reported in the following table.
- X-ray diffraction analysis indicates the product to be a novel crystalline material having an X-ray pattern of Table 1.
- Example 2 The procedure of Example 2 was repeated, using the same reaction composition, however, varying both the temperature and time of heat treatment.
- the temperatures employed were, respectively, 125° C. (51/2 days), 150° C. (8 days), and 175° C. (5 days).
- the results are reported in the table below.
- the calcined products of Examples 3-5 showed that substantially no change in crystal structure had occurred as a result of calcination.
- This example also illustrates a method for preparing Zeolite ZSM-5.
- 137.4 grams SiO 2 was partially dissolved in 648 ml. 2.18 N (CH 3 CH 2 CH 2 ) 4 NOH by heating to a temperature of about 100° C.
- the mixture was placed in a pyrex lined autoclave and heated at 150° C. for 9 days.
- the resultant solid product was cooled to room temperature, removed, filtered, washed with 2 liters H 2 O and dried at 230° F.
- a portion of this product was subjected to X-ray analysis and identified as ZSM-5.
- a portion of the subjected product was calcined at 1000° F. in air for 16 hours and the following analyses were obtained:
- Example 3 Samples of the product of Example 3 were subjected to ion exchange using various ion exchange solutions.
- the ion exchange solution was a saturated aqueous solution, at 180° F.
- the exchange was carried out batchwise using 500 ml. of saturated solution per gram of product.
- the exchanged products were than water washed until free of chloride.
- the samples were then tested for sorption characteristics. The details and results are reported in Table 10.
- Example 15 was repeated wherein samples of ZSM-5 were exchanged with 0.5 N HCl. Thereafter the so exchanged products were subjected to further ion exchange with either Na + , Ca + +, (RE) +++ , or Ag + (Examples 17-20, respectively). The results are set forth in Table 11.
- silica gel was dissolved in 238 grams 10% tetrapropylammonium hydroxide solution. To this was added with stirring the 1.6 gram NaAlO 2 (43.5 wt. percent Al 2 O 3 , 30.05 wt. percent Na 2 O) dissolved in 3 grams water. This mixture was then charged to an autoclave vessel and held at 149° C. for six days at autogenous pressure. The resulting product was separated from soluble components by filtering and washing, X-ray analysis of the dried (100-110° C.) sample showed the product to be crystalline ZSM-5.
- This example was prepared by first dissolving the tetrapropyl bromide (31.2 grams) and caustic (4.83 grams NaOH 77.5 wt. percent Na 2 O) in water. To this was added the sodium aluminate (1.6 grams NaAl 2 43.5% Al 2 O 3 -30.05 wt. percent Na 2 O) dissolved in some of the water. Finally, the silica component, commercial Ludox colloidal silica, 30% SiO 2 was added to the mixture. This mixture was charged to an autoclave and held at about 150° C. for six days at autogenous pressure. The resulting product, after filtering and washing, was shown by X-ray analysis to be crystalline ZSM-5.
- This example was prepared in a manner similar to that discussed under Example 23 differing only in the amount of caustic used and time of crystallization. X-ray analyses showed the product to be crystalline ZSM-5.
- ZSM-5 was prepared from tetrapropylammonium hydroxide and Ludox. 76.3 grams Ludox (30 wt. percent SiO 2 ) were added to 3.19 grams NaAlO 2 (42 wt. percent Al 2 O 3 , 35 wt. percent Na 2 O) dissolved in 99 ml. 2.37 N tetrapropylammonium hydroxide and 9 ml. H 2 O. A smooth, creamy gel formed immediately, which was mixed for three minutes. This was placed in Pyrex liner in an autoclave and run five days at 175° C. and autogenous pressure. The product was removed, filtered, washed once with one liter H 2 O, and dried at 230° F. Microscopic examination showed mainly crystalline material ⁇ 1 ⁇ . Reaction composition and product analysis are reported in Table 14.
- ZSM-5 was prepared from tetrapropylammonium bromide and sodium hydroxide. 3.19 grams NaAlO 2 (42 wt. percent Al 2 O 3 , 35 wt. percent Na 2 O) were dissolved in 9.44 grams NaOH in 60 ml. H 2 O. 63 grams tetrapropylammonium bromide were added and mixed until dissolved. 76.3 grams Ludox (30 wt. percent SiO 2 ) were then added hot and rapidly and mixed for five minutes. A thick, lumpy gel formed immediately. This was placed in a Pyrex liner in an autoclave and run eight days at 175° C. and autogenous pressure. A very hard product was removed, filtered, washed with 200 ml. H 2 O, and dried at 230° F. Microscopic examination showed mainly large rod-shaped crystals to 8 ⁇ 20 ⁇ , some large cubes to 25 ⁇ . Reaction composition and product analysis are reported in Table 14.
Abstract
Catalytic conversion of hydrocarbons is carried out by contacting the same with a family of crystalline zeolites designated as ZSM-having the composition expressed as mol ratios of oxides as follows:
0.9±M.sub.2/n O:Al.sub.2 O.sub.3 :ySiO.sub.2 :zH.sub.2 O
wherein M is at least one cation having a valence n, y is at least 5 and z is between 0-40, said aluminosilicates characterized by a specific X-ray powder diffraction pattern.
Description
This application is a continuation-in-part of Ser. No. 630,933, filed Apr. 14, 1967 and now abandoned and a division of Ser. No. 865,472, filed Oct. 10, 1969 now U.S. Pat. 3,702,886.
This invention relates to novel crystalline aluminosilicates and to methods for the preparation. More particularly, this invention relates to novel crystalline alumino-silicates having catalytic properties, to methods for preparing the same, and hydrocarbon conversion therewith.
Zeolitic materials, both natural and synthetic, have been demonstrated in the past to have catalytic capabilities for various types of hydrocarbon conversion. Certain zeolithic materials are ordered porous crystalline aluminosilicates having a definite crystalline structure within which there are a large number of small cavities which are interconnected by a number of still smaller channels. These cavities and channels are precisely uniform in size. Since the dimensions of these pores are such as to accept for adsorption molecules of certain dimensions while rejecting those of larger dimensions, these materials have come to be known as "molecular sieves" and are utilized in a variety of ways to take advantage of these properties.
Such molecular sieves include a wide variety of positive ion-containing crystalline aluminosilicates, both natural and synthetic. These aluminosilicates can be described as a rigid three-dimensional network of SiO4 and and AlO4 in which the tetrahedra are cross-linked by the sharing of oxygen atoms whereby the ratio of the total aluminum and silicon atoms to oxygen is 1:2. The electrovalence of the tetrahedra-containing aluminum is balanced by the inclusion in the crystal of a cation, for example, an alkali metal or an alkaline earth metal cation. This can be expressed by formula wherein the ratio of Al to the number of the various cations, such as Ca/2, Sr/2, Na, K, or Li, is equal to unity. One type of cation has been exchanged either in entirety or partially by another type of cation utilizing ion exchange techniques in a conventional manner. By means of such cation exchange, it has been possible to vary the size of the pores in the given aluminosilicate by suitable selection of the particular cation. The spaces between the tetrahedra are occupied by molecules of water prior to dehydration.
Prior art techniques have resulted in the formation of a great variety of synthetic crystalline aluminosilicates. These aluminosilicates have come to be designated by letter or other convenient symbol, as illustrated by zeolite A (U.S. 2,882,243), zeolite X (U.S. 2,882,244), zeolite Y (U.S. 3,130,007), zeolite K-G (U.S. 3,055,654), zeolite ZK-5 (U.S. 3,247,195), zeolite Beta (U.S. 3,308,069), and zeolite ZK-4 (U.S. 3,314,752), merely to name a few.
The present invention relates to a novel family of ultrastable synthetic siliceous crystalline materials, hereinafter designated as "Zeolite ZSM-5" or simply "ZSM-5" to methods for the preparation and to hydrocarbon conversion processes conducted therewith. The family of ZSM-5 comositions has the characteristic X-ray diffraction pattern set forth in Table 1, hereinbelow. ZSM-5 a compositions can also be identified, in terms of mole ratios of oxides, as follows:
0.9±0.2 M.sub.2/n O:W.sub.2 O.sub.3 :5-100YO.sub.2 :zH.sub.2 O
wherein M is a cation, n is the valence of said cation, W is selected from the group consisting of aluminum and gallium, Y is selected from the group consisting of silicon and germanium, and z is from 0 to 40. In a preferred synthesized form, the zeolite has a formula, in terms of mole ratios of oxides, as follows:
0.9±0.2 M.sub.2/n O:Al.sub.2 O.sub.3 :5-100SiO.sub.2 :zH.sub.2 O
and M is selected from the group consisting of a mixture of alkali metal cations, especially sodium, and tetraalkylammonium cations, the alkyl groups of which preferably contains 2-5 carbon atoms.
The original cations can be replaced in accordance with techniques well-known in the art, at least in part, by ion exchange with other cations. Preferred replacing cations include tetraalkylammonium cations, metal ions, ammonium ions, hydrogen ions, and mixtures of the same. Particularly preferred cations are those which render the zeolite catalytically active, especially for hydrocarbon conversion. These include hydrogen, rare earth metals, aluminum, metals of Groups II and VIII of the Periodic Table and manganese.
In a preferred embodiment of ZSM-5, W is aluminum, Y is silicon and the silica/alumina mole ratio is at least 10 and ranges up to about 60.
Members of the family of zeolites designated herein as ZSM-5 have an exceptionally high degree of thermal stability thereby rendering them particularly effective for use in processes involving elevated temperatures. In this connection, ZSM-5 zeolites appear to be one of the most stable families of zeolites known to date.
Members of the family of ZSM-5 zeolites possess a definite distinguishing crystalline structure whose X-ray diffraction pattern shows the following significant lines:
TABLE 1
______________________________________
Interplanar Spacing d (A):
Relative intensity
______________________________________
11.1 ± 0.2 S
10.0 ± 0.2 S
7.4 ± 0.15 W
7.1 ± 0.15 W
6.3 ± 0.1 W
6.04
± 0.1 W
5.97
5.56 ± 0.1 W
5.01 ± 0.1 W
4.60 ± 0.08
4.60 ±
4.25 ± 0.08 W
3.85 ± 0.07 VS
3.71 ± 0.05 S
3.04 ± 0.03 S
2.99 ± 0.02 W
2.94 ± 0.02 W
______________________________________
These values were determined by standard techniques. The radiation was the K-alpha doublet of copper, and a scintillation counter spectrometer with a strip chart pen recorder was used. The peak heights, I, and the positions as a function of 2 time theta, where theta is the Bragg angle, were read from the spectrometer chart. From these, the relative intensities, 100I/Io, where Io is the intensity of the strongest line or peak, and d (obs), the interplanar spacing in A. corresponding to the recorded lines, were calculated. In Table I the relative intensities are given in terms of the symbols S=strong, M=medium, MS=medium strong, MW=medium weak and VS=very strong. It should be understood that this X-ray diffraction pattern is characteristic of all the species of ZSM-5 compositions. Ion exchange of the sodium ion with cations reveals substantially the same pattern with some minor shifts in interplanar spacing and variation in relative intensity. Other minor variations can occur depending on the silicon to aluminum ratio of the particular sample, as well as if it has been subjected to thermal treatment. Various cation exchanged forms of ZSM-5 have been prepared. X-ray powder diffraction patterns of several of these forms are set forth below. The ZSM-5 forms set forth below are all aluminosilicates.
TABLE 2
______________________________________
X-ray diffraction; ZSM-5 powder in cation exchanged forms;
d Spacings observed
As
made HCl NaCl CaCl.sub.3
ReCl.sub.3
AgNO.sub.3
______________________________________
11.15 11.16 11.19 11.19 11.19 11.19
10.01 10.03 10.05 10.01 10.06 10.01
9.74 9.78 9.80 9.74 9.79 9.77
-- -- 9.01 9.02 -- 8.99
8.06 -- -- -- -- --
7.44 7.46 7.46 7.46 7.40 7.76
7.08 7.07 7.09 7.11 -- 7.09
6.70 6.72 6.73 6.70 6.73 6.73
6.36 6.38 6.38 6.37 6.39 6.37
5.99 6.00 6.01 5.99 6.02 6.01
5.70 5.71 5.73 5.70 5.72 5.72
5.56 5.58 5.58 5.57 5.59 5.58
5.37 -- 5.38 5.37 5.38 5.37
5.13 5.11 5.14 5.12 5.14 --
4.99 5.01 5.01 5.01 5.01 5.01
-- -- 4.74 -- -- --
4.61 4.62 4.62 4.61 4.63 4.62
-- -- 4.46 4.46 -- 4.46
4.36 4.37 4.37 4.36 4.37 4.37
4.26 4.27 4.27 4.26 4.27 4.27
4.08 -- 4.09 4.09 4.09 4.09
4.00 4.01 4.01 4.00 4.01 4.01
3.84 3.85 3.85 3.85 3.86 3.86
3.82 3.82 3.82 3.82 3.83 3.82
3.75 3.75 3.75 3.76 3.76 3.75
3.72 3.72 3.72 3.72 3.72 3.72
3.64 3.65 3.65 3.65 3.65 3.65
3.60 3.60 3.60 3.61 3.60
3.48 3.49 3.49 3.48 3.49 3.49
3.44 3.45 3.45 3.44 3.45 3.45
3.34 3.35 3.36 3.35 3.35 3.35
3.31 3.31 3.32 3.31 3.32 3.32
3.25 3.25 3.26 3.25 3.25 3.26
3.17 -- -- 3.17 3.18 --
3.13 3.14 3.14 3.14 3.15 3.14
3.05 3.05 3.05 3.04 3.06 3.05
2.08 2.08 2.99 2.93 2.99 2.99
-- -- -- -- 2.97 --
2.95 2.95 2.94 2.95 2.95
2.86 2.87 2.87 2.87 2.87 2.87
2.80 -- -- -- -- --
2.78 -- -- 2.78 -- 2.78
2.73 2.74 2.74 2.73 2.74 2.74
2.67 -- -- 2.68 -- --
2.66 -- -- 2.65 -- --
2.60 2.61 2.61 2.61 2.61 2.61
2.59 -- 2.59 -- --
2.57 -- 2.57 2.56 -- 2.57
2.50 2.52 2.52 2.52 2.52 --
2.49 2.49 2.49 2.49 2.49 2.49
-- -- -- 2.45 -- --
2.41 2.42 2.42 2.42 2.42 --
2.39 2.40 2.40 2.39 2.40 2.40
-- -- -- 2.38 2.35 2.38
2.33 -- 2.33 2.32 2.33
2.30 -- -- -- --
2.24 2.23 2.23 -- --
2.20 2.21 2.20 2.20 --
2.18 2.18 -- -- --
-- 2.17 2.17 -- --
2.13 -- 2.13 -- --
2.11 2.11 -- 2.11 --
-- -- 2.10 2.10 --
2.08 2.08 -- 2.08 2.08
-- 2.07 2.07 2.07 --
-- -- 2.04 -- --
2.01 2.01 2.01 2.01 2.01 2.01
1.99 2.00 1.99 1.99 1.99 1.99
-- -- 1.97 1.96 --
1.95 1.95 1.95 1.95 1.95 --
-- -- -- 1.94 --
1.92 1.92 1.92 1.92 1.92
1.91 -- -- -- 1.91 --
-- -- -- 1.88 --
1.87 1.87 1.87 1.87 1.87 1.87
1.86 -- -- -- --
1.84 1.84 -- -- 1.84 1.84
1.83 1.83 1.83 1.83 1.83 --
1.82 -- 1.81 -- 1.82 --
1.77 1.77 1.79 1.78 -- 1.77
1.76 1.76 1.76 1.76 1.76 1.76
-- 1.75 -- -- 1.75
1.74 1.74 1.73 -- --
1.71 1.72 1.72 1.71 -- 1.70
1.67 1.67 1.67 -- 1.67 1.67
1.66 1.66 -- 1.66 1.66 1.66
-- 1.65 1.65 -- --
-- 1.64 1.64 -- --
1.63 1.63 1.63 1.63 1.62
1.61 1.61 1.61 -- 1.61
1.58 -- -- -- -- --
1.57 1.57 -- 1.57 1.57
-- 1.56 1.56 1.56 --
______________________________________
While ZSM-5 zeolites are useful in cracking and hydrocracking, they are outstandingly useful in other petroleum refining processes indicating again the unique catalytic characteristics of this family of zeolites. The later processes include isomerization of n-paraffins and naphthenes, polymerization of compounds containing an olefinic or acetylinic carbon to carbon linkage such as isobutylene and butene-1, reforming, alkylation, isomerization of polyalkyl substituted aromatics, e.g., ortho xylene and disproportionation of aromatics, such as toluene to provide a mixture of benzene, xylenes and higher methylbenzenes. The ZSM-5 catalysts have exceptional high selectivity and under the conditions of hydrocarbon conversion provide a high percentage of desired products relative to total products compared with known zeolitic hydrocarbon conversion catalysts.
ZSM-5 zeolites, as indicated above, are also useful in other catalytic processes, such as catalytic cracking of hydrocarbons and hydrocracking. In addition to the thermal stability of this family of zeolites under these conditions, they provide conversion of the cracked oil to materials having lower molecular weights and boiling points which are of greater economic value. The ability to be physically stable under high temperatures and/or in the presence of high temperature steam is extremely important for a cracking catalyst. During catalytic conversion, the reaction which takes place is essentially a cracking to produce hydrocarbons. However, this cracking is accompanied by a number of complex side reactions such as aromatization, polymerization, alkylation and the like. As a result of these complex reactions, a carbonaceous deposit is laid down on the catalyst which is referred to by petroleum engineers as "coke." The deposit of coke on the catalyst tends to seriously impair the catalyst efficiency for the principal reaction desired and to substantially decrease the rate of conversion and/or the selectivity of the process. Thus, it is common to remove the catalyst after coke has been deposited thereon and to regenerate it by burning the coke in a stream of oxidizing gas. The regenerated catalyst is returned to the conversion stage of the process cycle. The enhanced thermal stability of ZSM-5 is advantageous in this regard.
ZSM-5 zeolites can be used either in the alkali metal form, e.g., the sodium form, the ammonium form, the hydrogen form, or another univalent or multivalent cationic form. Preferably, one or other of the last two forms is employed. They can also be used in intimate combination with a hydrogenating component such as tungsten, vanadium, molybdenum, rhenium, nickel, cobalt, chromium, manganese, or a noble metal such as platinum or palladium where a hydrogenation dehydrogenation function is to be performed. Such component can be exchanged into the composition, impregnated therein or physically intimately admixed therewith. Such component can be impregnated in or on to ZSM-5 such as, for example, by, in the case of platinum, treating the zeolite with a platinum metal-containing ion. Thus, suitable platinum compounds include chloroplatinic acid, platinous chloride and various compounds containing the platinum ammine complex.
The compounds of the useful platinum or other metals can be divided into compounds in which the metal is present in the cation of the compound and compounds in which it is present in the anion of the compound. Both types of compounds which contain the metal in the ionic state can be used. A solution in which platinum metals are in the form of a cation or cationic complex, e.g.,
Pt(NH.sub.3).sub.6 Cl.sub.4
is particularly useful. For some hydrocarbon conversion processes, this noble metal form of the ZSM-5 catalyst is unnecessary such as in low temperature, liquid phase ortho xylene isomerization.
ZSM-5, when employed either as an adsorbent or as a catalyst in one of the aforementioned processes, should be dehydrated at least partially. This can be done by heating to a temperature in the range of 200 to 600° C. in an atmosphere such as air, nitrogen, etc. and at atmospheric or subatmospheric pressures for between 1 and 48 hours. Dehydration can aso be performed at lower temperatures merely by placing the ZSM-5 catalyst in a vacuum, but a longer time is required to obtain a sufficient amount of dehydration.
Zeolite ZSM-5 can be suitably prepared by preparing a solution containing tetrapropyl ammonium hydroxide, sodium oxide, an oxide of aluminum or gallium, an oxide or silica or germanium, and water and having a composition, in terms of mole ratios of oxides, falling within the following ranges:
TABLE 3
______________________________________
Particularly
Broad Preferred preferred
______________________________________
OH-/YO.sub.2 0.07-10.0
0.1-0.8 0.2-0.75
R.sub.4 N+/(R.sub.4 N.sup.++Na.sup.+)
0.2-0.95
0.3-0.9 0.4-0.9
H.sub.2 /OH 10-300 10-300 10-300
YO.sub.2 /W.sub.2 O.sub.3
5-100 10-60 10-40
______________________________________
wherein R is propyl, W is aluminum or gallium and Y is silicon or germanium maintaining the mixture until crystals of the zeolite are formed. It is noted that an excess of tetrapropylammonium hydroxide can be used which would raise the value of OH-/YO2 above the ranges set forth supra. The excess hydroxide, of course, does not participate in the reaction. Thereafter, the crystals are separated from the liquid and recovered. Typical reaction conditions consist of heating the foregoing reaction mixture to a temperature of from about 100° C. to 175° C. for a period of time of from about six hours to 60 days. A more preferred temperature range is from about 150° to 175° C. with the amount of time at a temperature in such range being from about 12 hours to 8 days.
The digestion of the gel particles is carried out until crystals form. The solid product is separated from the reaction medium, as by cooling the whole to room temperature, filtering, and water washing.
The foregoing product is dried, e.g., at 230° F., for from about 8 to 24 hours. Of course, milder conditions may be employed if desired, e.g., room temperature under vacuum.
ZSM-5 is preferably formed as an aluminosilicate. The composition can be prepared utilizing materials which supply the appropriate oxide. Such compositions include for an aluminosilicate, sodium aluminate, alumina, sodium silicate, silica hydrosol, silica gel, silicic acid, sodium hydroxide and tetrapropylammonium compounds, e.g., tetrapropylammonium hydroxide. It will be understood that each oxide component utilized in the reaction mixture for preparing a member of the ZSM-5 family can be supplied by one of more initial reactants and they can be mixed together in any order. For example, sodium oxide can be supplied by an aqueous solution of sodium hydroxide, or by an aqueous solution of sodium silicate; tetrapropylammonium cation can be supplied by the bromide salt. The reaction mixture can be prepared either batchwise or continuously. Crystal size and crystallization time of the ZSM-5 composition will vary with the nature of the reaction mixture employed.
Members of the ZSM-5 family can have the original cations associated therewith replaced by a wide variety of other cations according to techniques well known in the art. Typical replacing cations would include hydrogen, ammonium and metal cations including mixtures of the same. Of the replacing metallic cations, particular preference is given to cations of metals such as rare earth metals, manganese, calcium, as well as metals of Group II of the Periodic Table, e.g., zinc, and Group VIII of the Periodic Table, e.g., nickel.
Typical ion exchange techniques would be to contact the members of the family of ZSM-5 zeolites with a salt of the desired replacing cation or cations. Although a wide variety of salts can be employed, particular preference is given to chlorides, nitrates and sulfates.
Representative ion exchange techniques are disclosed in a wide variety of patents including U.S. 3,140,249; U.S. 3,140,251; and U.S. 3,140,253.
Following contact with the salt solution of the desired replacing cation, the zeolites are then preferably washed with water and dried at a temperature ranging from 150° F. to about 600° F. and thereafter calcined in air or other inert gas at temperatures ranging from about 500° F. to 1500° F. for periods of time ranging from 1 to 48 hours or more.
Regardless of the cations replacing the sodium in the synthesized form of the ZSM-5 the spatial arrangement of the aluminum, silicon and oxygen atoms which form the basic crystal lattices of ZSM-5, remains essentially unchanged by the described replacement of sodium or other alkali metal as determined by taking an X-ray powder diffraction pattern of the ion-exchanged material. Such X-ray diffraction pattern of the ion-exchanged ZSM-5 reveals a pattern substantially the same as that set forth in Table 1 above.
The aluminosilicates prepared by the instant invention are formed in a wide variety of particular sizes. Generally speaking, the particles can be in the form of a powder, a granule, or a molded product, such as extrudate having particle size sufficient to pass through a 2 mesh (Tyler) screen and be retained on a 400 mesh (Tyler) screen. In cases where the catalyst is molded, such as by extrusion, the aluminosilicate can be extruded before drying or dried or partially dried and then extruded.
In the case of many catalysts, it is desired to incorporate the ZSM-5 with another material resistant to the temperatures and other conditions employed in organic conversion processes. Such materials include active and inactive materials and synthetic or naturally occurring zeolites as well as inorganic materials such as clays, silica and/or metal oxides. The latter may be either naturally occurring or in the form of gelatinous precipitates or gels including mixtures of silica and metal oxides. Use of a material in conjunction with the ZSM-5, i.e., combined therewith which is active, tends to improve the conversion and/or selectivity of the catalyst in certain organic conversion processes. Inactive materials suitably serve as diluents to control the amount of conversion in a given process so that products can be obtained economically and orderly without employing other means for controlling the rate of reaction. Normally, zeolite materials have been incorporated into naturally occurring clays, e.g., bentonite and kaolin, to improve the crush strength of the catalyst under commercial operating conditions. These materials, i.e., clays, oxides, etc., function as binders for the catalyst. It is desirable to provide a catalyst having good crush strength, because in a petroleum refinery the catalyst is often subjected to rough handling, which tends to break the catalyst down into powder-like materials which cause problems in processing. These clay binders have been employed for the purpose of improving the crush strength of the catalyst.
Naturally occurring clays which can be composited with the ZSM-5 catalyst include the montmorillonite and kaolin family, which families include the sub-bentonites, and the kaolins commonly known as Dixie McNamee-Georgia and Florida clays or others in which the main mineral constituent is halloysite, kaolinite, dickite, nacrite, or anauxite. Such clays can be used in the raw state as originally mined or initially subjected to calcination, acid treatment or chemical modification.
In addition to the foregoing materials the ZSM-5 catalyst can be composited with a porous matrix material such as silica-alumina, silica-magnesia, silica-zirconia, silica-thoria, silica-beryllia, silica-titania as well as ternary compositions such as silica-alumina-thoria, silica-alumina-zirconia, silica-alumina-magnesia and silica-magnesia-zirconia. The matrix can be in the form of a cogel. The relative proportions of finely divided crystalline alumino-silicate ZSM-5 and inorganic oxide gel matrix vary widely with the crystalline aluminosilicate content ranging from about 1 to about 90 percent by weight and more usually, particularly when the composite is prepared in the form of beads in the range of about 2 to about 50 percent by weight of the composite.
Employing the ZSM-5 catalyst of this invention, containing a hydrogenation component, heavy petroleum residual stocks, cyclic stocks, and other hydrocrackable charge stocks can be hydrocracked at temperatures between 400° F. and 825° F. using molar ratios of hydrogen to hydrocarbon charge in the range between 2 and 80. The pressure employed will vary between 10 and 2,500 p.s.i.g. and the liquid hourly space velocity between 0.1 and 10.
Employing the catalyst of this invention for catalytic cracking hydrocarbon cracking stocks can be cracked at a liquid hourly space velocity between about 0.5 and 50, a temperature between about 550° F. and 1100° F., a pressure between about subatmospheric and several hundred atmospheres.
Employing a catalytically active form of a member of the ZSM-5 family of zeolites of this invention containing a hydrogenation component, reforming stocks can be reformed employing a temperature between 700° F. and 1000° F. The pressure can be between 100 and 1000 p.s.i.g. but is preferably between 200 and 700 p.s.i.g. The liquid hourly space velocity is generally between 0.1 and 10, preferably between 0.5 and 4 and the hydrogen to hydrocarbon mole ratio is generally between 1 and 20 preferably between 4 and 12.
The catalyst can also be used for hydroisomerization of normal paraffins, when provided with a hydrogenation component, e.g., platinum. Hydroisomerization is carried out at a temperature between 200 and 700° F., preferably 300 to 550° F., with a liquid hourly space velocity between 0.01 and 2, preferably between 0.25 and 0.50 employing hydrogen such that the hydrogen to hydrocarbon mole ratio is between 1:1 and 5:1. Additionally, the catalyst can be used for olefin isomerization employing temperatures between 30° F. and 500° F.
Other reactions which can be accomplished employing the catalyst of this invention containing a metal, e.g., platinum, include hydrogenation-dehydrogenation reactions and desulfurization reactions.
In order to more fully illustrate the nature of the invention and the manner of practicing the same, the following examples are presented.
In the examples which follow whenever adsorption data is set forth it was determined as follows:
A weighed sample of the zeolite was contacted with the desired pure adsorbate vapor in an adsorption chamber at a pressure less than the vapor-liquid equilibrium pressure of the adsorbate at room temperature. This pressure was kept constant during the adsorption period which did not exceed about eight hours. Adsorption was complete when a constant pressure in the adsorption chamber was reached, i.e., 12 mm. of mercury for water and 20 mm. for n-hexane and cyclohexane. The increase in weight was calculated as the adsorption capacity of the sample.
This example illustrates the preparation of zeolite ZSM-5. 22.9 grams SiO2 was partially dissolved in 100 ml. 2.18 N tetrapropylammonium hydroxide by heating to a temperature of about 100° C. There was then added a mixture of 3.19 grams NaAlO2 (comp: 42.0 wt. percent Al2 O3, 30.9 wt. percent Na2 O, 27.1 wt. percent H2 O) dissolved in 53.8 ml. H2 O. The resultant mixture had the following composition: 0.382 mole SiO2, 0.0131 mole Al2 O3, 0.0159 mole Na2 O, 0.118 mole [(CH3 CH2 CH2)4 N]2 O, 6.30 moles H2 O. The mixture was placed in a Pyrex lined autoclave and heated at 150° C. for six days. The resultant solid product was cooled to room temperature, removed, filtered, washed with 1 liter H2 O and dried at 230° F. A portion of this product was subjected to X-ray analysis and identified as ZSM-5. A portion of the product was calcined at 1000° F. in air for 16 hours and the following analyses were obtained:
TABLE 4
______________________________________
Wt. percent SiO.sub.2 93.62
Wt. percent Al.sub.2 O.sub.3
4.9
Wt. percent Na.sub.2 O 1.48
Total 100.00
SiO.sub.2 /Al.sub.2 O.sub.3
32.5
Na.sub.2 O/Al.sub.2 O.sub.3
0.5
Wt. percent n-hexane adsorbed
10.87
Wt. percent cyclohexane adsorbed
3.60
Wt. percent H.sub.2 O adsorbed
9.15
______________________________________
This example illustrates another preparation of Zeolite ZSM-5. 22.9 grams of SiO2 were partially dissolved in 85.5 ml. of 2.21 N (CH3 CH2 CH2)4 NOH by heating to a temperature of about 100° C. There was then added a mixture of 2.86 grams of sodium aluminate (44.5 weight percent Al2 O3, 30.1 percent Na2 O, 25.4 percent H2 O) dissolved in 53.8 ml. water and 0.07 gram aluminum turnings (to maintain the Si/Al molar ratio) dissolved in 21 ml. of 2.21 N (CH3 CH2 CH2)4 NOH.
The resultant mixture had the following composition: 0.382 mole SiO2, 0.0138 mole Al2 O3, 0.0139 mole Na2 O, 0.236 mole (CH3 CH2 CH2)4 NOH, and 6.25 moles H2 O. This composition was placed in a Pyrex lined autoclave, heated to 150° C., and maintained at this temperature for five days. The resultant solid product was cooled to room temperature, removed, filtered and washed with 1 liter of water. The product was both grainy and dilatant. Microscopic examination showed the presence of very small crystals (on the order of 1 micron) along with some gel particles. The product was then calcined at 1000° F. The analysis of this product is reported in the following table.
TABLE 5
______________________________________
Preparation of ZSM-5 at 150° C.
Reaction composition (moles):
SiO.sub.2 0.382
Al.sub.2 O.sub.3 0.0138
Na.sub.2 O 0.139
(CH.sub.3 CH.sub.2 CH.sub.2).sub.4 NOH
0.236
H.sub.2 O 6.25
Products:
Na, wt. percent 2.03
Al.sub.2 O.sub.3, wt. percent 5.07
SiO.sub.2, wt. percent 92.7
SiO.sub.2 /Al.sub.2 O.sub.3 31.1
Na.sub.2 O/Al.sub.2 O.sub.3 0.89
Sorption properties of product:
Wt. percent cyclohexane
percent 3.3
n-Hexane do. 9.7
Water do. 8.3
______________________________________
X-ray diffraction analysis indicates the product to be a novel crystalline material having an X-ray pattern of Table 1.
The procedure of Example 2 was repeated, using the same reaction composition, however, varying both the temperature and time of heat treatment. Thus, the temperatures employed were, respectively, 125° C. (51/2 days), 150° C. (8 days), and 175° C. (5 days). The results are reported in the table below. The calcined products of Examples 3-5 showed that substantially no change in crystal structure had occurred as a result of calcination.
TABLE 6
______________________________________
Preparation of ZSM-5
Example
3 4 5
______________________________________
Time, days 8 51/2 5
Temperature, ° C
150 125 175
Reaction composition:
Moles:
SiO.sub.2 0.382 0.382 0.38
Al.sub.2 O.sub.3 0.138 0.138 0.138
Na.sub.2 O 0.0139 0.0139 0.0139
(C.sub.3 CH.sub.2 CH.sub.2).sub.4 NOH
0.236 0.236 0.236
H.sub.2 O 6.25 6.25 6.25
Product:.sup.1
Na, wt. percent 1.7 2.1 1.6
Na.sub.2 O, wt. percent
2.29 2.82 2.15
Al.sub.3 O.sub.3, wt. percent
4.47 3.55 4.3
SiO.sub.2, wt. percent
93.30 93.7 93.2
Total, as oxides 100.1 100.1 99.65
SiO.sub.2 /Al.sub.2 O.sub.3
35.5 45.0 37.0
Na.sub.2 O/Al.sub.2 O.sub.3
0.86 1.31 0.83
Physical properties-Adsorption:
Cyclohexane, wt. percent
3.63 5.83 2.52
H.sub.2 O, wt. percent
9.52 7.33 9,48
n-C.sub.5, wt. percent
9.81 9.67 10.10
______________________________________
.sup.1 Calcined 1,000° F.
As can be seen from the above table, the calcined crystalline products obtained in Examples 3-5 were investigated in order to ascertain whether these products exhibited selective absorption properties. It will be noted that the data shows that the crystalline aluminosilicate zeolites of the present invention absorb more straight chain paraffins than cyclic aliphatics.
This example also illustrates a method for preparing Zeolite ZSM-5. 137.4 grams SiO2 was partially dissolved in 648 ml. 2.18 N (CH3 CH2 CH2)4 NOH by heating to a temperature of about 100° C. There was then added a mixture of 19.08 grams NaAlO2 (composition: 42.0 wt. percent Al2 O3, 30.9% Na2 O, 27.1% H2 O) dissolved in 322.5 ml. H2 O. The mixture was placed in a pyrex lined autoclave and heated at 150° C. for 9 days. The resultant solid product was cooled to room temperature, removed, filtered, washed with 2 liters H2 O and dried at 230° F. A portion of this product was subjected to X-ray analysis and identified as ZSM-5. A portion of the subjected product was calcined at 1000° F. in air for 16 hours and the following analyses were obtained:
______________________________________
Wt. percent SiO.sub.2
94.6
Wt. percent Al.sub.2 O.sub.3
3.8
Wt. percent Na.sub.2 O
1.93
Total 100.33
______________________________________
Sorption and other data are set forth in Table 7.
TABLE 7
______________________________________
Physical Properties:
Surface area, m..sup.2 /g.
299
Sorption:
Cyclohexane, wt. percent
3.32
n-Hexane, wt. percent
9.50
Water, wt. percent 6.18
X-ray analysis:
Type ZSM-5
Crystallinity; percent
100
______________________________________
In order to investigate the thermal stability of the Zeolite of Example 6, five portions of the same were subjected to direct calcination in air at temperatures of 1000, 1500, 1600, 1700, and 1850° F., respectively. The crystal structure remained stable at each of the first four temperatures. At 1850° F. some decrease in crystallinity was observed, probably due to sintering at this higher temperature. Results are shown in Table 8.
TABLE 8
______________________________________
Thermal stability of ZSM-5
Calculation Temp.:
° F 1,000 1,500 1,600
1,700
1.850
° C 838 815 871 927 1,010
Calcined 10 hours in air
Adsorption:
Normal hexane, wt. percent
9.50 8.80 8.23 8.80 2.05
Water, wt. percent
6.18 4.02 3.67 3.20 0.78
X-ray analysis:
crystallinity, percent
100 100 100 100 65
______________________________________
Inasmuch as the crystalline aluminosilicate zeolites of this invention are characterized by a rather high silica/alumina ratio, it was postulated that they would have an unusually stable structure. Accordingly, a series of alternating water sorptions and calcinations at 1000° F. was carried out using about 1 gram of the product obtained in Example 3. The results are summarized in Table 9. It will be noted that the hydrothermal treatments did not have any adverse effect on the water adsorption properties.
TABLE 9
______________________________________
Hydrothermal stability of ZSM-5
[Description, calcined at 1,000° F.]
Calci-
nation
treat-
Number of sorption
ments 1 2 3 4 5
______________________________________
Adsorption:
H.sub.2 O, wt. percent
7.85 7.83 7.50 7.54 7.67 8.00
Cyclohexane,wt.percent
4.45
n-Hexane, wt. percent
10.31
______________________________________
Samples of the product of Example 3 were subjected to ion exchange using various ion exchange solutions. In each instance, the ion exchange solution was a saturated aqueous solution, at 180° F. The exchange was carried out batchwise using 500 ml. of saturated solution per gram of product. The exchanged products were than water washed until free of chloride. The samples were then tested for sorption characteristics. The details and results are reported in Table 10.
TABLE 10
__________________________________________________________________________
Ion-exchanged forms of ZSM-5
Example number
8.sup.a
9.sup.b
10.sup.c
11.sup.c
12.sup.c
13.sup.c
14.sup.c
15.sup.c
__________________________________________________________________________
Ion exchanged-Saturated solutions at 180° F
AgNO.sub.3
AgNO.sub.3
CaCl.sub.2
NH.sub.4 Cl
ReCl.sub.3
NaCl
0.5 NHCl
Composition:
Na, wt. percent 1.7 0.46 0.12 <0.05
<0.05
1.2 1.37
0.22
Na.sub.2 O, wt. percent
2.29
0.62 0.16 1.62
1.94
0.30
Al.sub.2 O.sub.3, wt. percent
4.47
2.90 2.62 2.84
6.25
6.53
3.20
3.45
SiO.sub.2, wt. percent
93.30
93.56
91.60
94.80
90.30
88.50
93.80
96.10
Total, as oxides 100.06 100.22
98.72
96.55
98.42
98.84
90.85
SiO.sub.2 /Al.sub.2 O.sub.3 (molar ratio)
35.5
60.7 59.5 56.8
24.6
22.8
49.7
47.4
Equivalents M/g, atom aluminum
0.86 1.08 0.63 0.48
0.95
0.015
Physical properties-Adsorption:
Cyclohexane, wt. percent
3.63
n-Hexane, wt. percent
9.81 9.48 10.34
11.08
9.62
9.72
10.77
H.sub.2 O, wt. percent
9.52 6.37 7.16
8.83
7.33
8.13
7.50
X-ray analysis Crystalline material
Exchanged ion, wt. percent
2.12 5.43 0.88 1.72
Ag Ag ca Re.sub.2 O.sub.3
__________________________________________________________________________
.sup.a 8 days at 150° C.; calcined at 1,000° F.
.sup.b Dried at 230° F.
.sup.c Calcined at 1,000° F.
Example 15 was repeated wherein samples of ZSM-5 were exchanged with 0.5 N HCl. Thereafter the so exchanged products were subjected to further ion exchange with either Na+, Ca+ +, (RE)+++, or Ag+ (Examples 17-20, respectively). The results are set forth in Table 11.
TABLE 11
__________________________________________________________________________
ZSM-5 (0.5N HCl treated, calcined at 1000° F.
__________________________________________________________________________
example number
16 17 18 18 20
__________________________________________________________________________
Treatment (1) (1) (1) (1) (1)
Ion exchanged-Saturated
solutions at 180° F
NaCl
CaCl.sub.2
ReCl.sub.3
AgNO.sub.3
Composition, wt. percent:
Re.sub.2 O.sub.3 1.60
CaO 0.14
Ag.sub.2 O 6.07
Al.sub.2 O.sub.3
2.95 2.58
2.62 2.91 3.10
SiO.sub.2 97.1 95.0
97.5 94.4 91.4
Total, as oxides
100.2
99.2
100.8
99.7 100.7
Moles SiO.sub.2 /Al.sub.2 O.sub.3
56 63 63 55 50
Equivalents M/aluminum
0.1 1.05
0.46 0.60 0.91
Adsorption, wt. percent:
n-Hexane 10.92
8.85
9.64 10.27
9.82
Water 7.96 6.90
7.18 7.52 5.92
X-ray analysis
Crystalline material
__________________________________________________________________________
.sup.1 0.5 N HCl treated, calcined at 1,000° F.
The initial exchange with 0.5 N HCl resulted in a highly crystalline product which did not appear to contain amorphous material.
A product made as described in Example 15, wherein ZSM-5 was ion-exchanged with 0.5 N HCl was tested for cracking activity using n-hexane. The results are reported in Table 12.
TABLE 12
______________________________________
Catalytic cracking activity of ZSM-5 zeolite
______________________________________
Composition:
Wt. percent SiO.sub.2 92.9
Wt. percent Al.sub.2 O.sub.3
5.04
Wt. percent Na 0.44
Sorption, wt. percent: Unsteamed
n-Hexane 10.2
Water 8.2
Cyclohexane 3.1
Unsteamed
Alpha value .sup.1 680
n-Hexane conversion (percent)
.sup.2 99.3
______________________________________
.sup.1 The alpha test is a measure of cracking activity. This test is
decribed in a letter to the editor entitled "Superactive Crystalline
Aluminosilicate Hydrocarbon Crackking Catalysts" by P. B. Weisz and J. N.
Minle, Journal of Catalyst, vol. 4, No. 4, August 1965, pp. 527-520.
.sup.2 At 800° F.
The following examples serve to demonstrate that ZSM-5 can be prepared using tetrapropylammonium bromide (TPABR) instead of tetrapropylammonium hydroxide. In addition, another example (22) was performed using silica gel as a source of silica. Preparational details of each of these examples are given below and summarized in Table 13.
In preparing this example 11.45 grams silica gel was dissolved in 238 grams 10% tetrapropylammonium hydroxide solution. To this was added with stirring the 1.6 gram NaAlO2 (43.5 wt. percent Al2 O3, 30.05 wt. percent Na2 O) dissolved in 3 grams water. This mixture was then charged to an autoclave vessel and held at 149° C. for six days at autogenous pressure. The resulting product was separated from soluble components by filtering and washing, X-ray analysis of the dried (100-110° C.) sample showed the product to be crystalline ZSM-5.
This example was prepared by first dissolving the tetrapropyl bromide (31.2 grams) and caustic (4.83 grams NaOH 77.5 wt. percent Na2 O) in water. To this was added the sodium aluminate (1.6 grams NaAl2 43.5% Al2 O3 -30.05 wt. percent Na2 O) dissolved in some of the water. Finally, the silica component, commercial Ludox colloidal silica, 30% SiO2 was added to the mixture. This mixture was charged to an autoclave and held at about 150° C. for six days at autogenous pressure. The resulting product, after filtering and washing, was shown by X-ray analysis to be crystalline ZSM-5.
This example was prepared in a manner similar to that discussed under Example 23 differing only in the amount of caustic used and time of crystallization. X-ray analyses showed the product to be crystalline ZSM-5.
TABLE 13
__________________________________________________________________________
ZSM-5 preparations from TEPABr
__________________________________________________________________________
Examples
22 23 24
__________________________________________________________________________
Formulation:
SiO.sub.2 gel, g
11.45
Ludox (LS), g 38.17 38.17
NaAlO.sub.2.sup.2, g
1.6 1.6 1.6
NaOH.sup.3,g 4.83 1.3
H.sub.2 O, g
3.0 200 200
10% TPAOH.sup.4, g
238
TPABr, g 31.21 312.1
Mole ratios:
SiO.sub.2 28 27.93 27.93
Al.sub.2 O.sub.3
1.0 1.0 1.0
Na.sub.2 O 1.04 9.90 3.52
(R.sub.4 N).sub.2 O
8.56
H.sub.2 O 1,730 1,847.5
1,847.5
R.sub.4 N.sup.+
17.1 17.0 17.0
Na.sup.+ 2.08 19.97 7.04
OH.sup.- 19.18 19.97 7.04
[Na.sub.2 O + (R.sub.4 N).sub.2 O]SiO.sub.2
0.343
R.sub.4 N.sup.+ /(R.sub.4 N.sup.+ + Na.sup.+)
0.892 .4508 .707
OH.sup.- /SiO.sub.2
0.685 .715 .2521
H.sub.2 O/[(R.sub.4 N).sub.2 O + Na.sub.2 O]
180
H.sub.2 O/(R.sub.4 N.sup.+ + Na.sup.+)
88 49.97 76.85
H.sub.2 O/OH.sup.-
88 49.97 76.85
SiO.sub.2 /Al.sub.2 O.sub.3
27.93 27.93
Crystallizaton:
24 hr 100% ZSM-5
60 hr 100% ZSM-5
6 days 60% ZSM-5
95% ZSM-5
7 days
Product analysis, moles:
SiO.sub.2 11.7 83.5
Al.sub.2 O.sub.3
1.0 1.0
Na.sub.2 O 0.48 0.63
(R.sub.4 N).sub.2 O
0.63 5.55
__________________________________________________________________________
.sup.1 30% SiO.sub.2.
.sup.2 Al.sub.2 O.sub.3 wt. percent 43.5 Na.sub.2 O 30.05.
.sup.3 NaOH 77.5% Na.sub.2 O.
.sup.4 10% water solution.
ZSM-5 was prepared from tetrapropylammonium hydroxide and Ludox. 76.3 grams Ludox (30 wt. percent SiO2) were added to 3.19 grams NaAlO2 (42 wt. percent Al2 O3, 35 wt. percent Na2 O) dissolved in 99 ml. 2.37 N tetrapropylammonium hydroxide and 9 ml. H2 O. A smooth, creamy gel formed immediately, which was mixed for three minutes. This was placed in Pyrex liner in an autoclave and run five days at 175° C. and autogenous pressure. The product was removed, filtered, washed once with one liter H2 O, and dried at 230° F. Microscopic examination showed mainly crystalline material <1μ. Reaction composition and product analysis are reported in Table 14.
ZSM-5 was prepared from tetrapropylammonium bromide and sodium hydroxide. 3.19 grams NaAlO2 (42 wt. percent Al2 O3, 35 wt. percent Na2 O) were dissolved in 9.44 grams NaOH in 60 ml. H2 O. 63 grams tetrapropylammonium bromide were added and mixed until dissolved. 76.3 grams Ludox (30 wt. percent SiO2) were then added hot and rapidly and mixed for five minutes. A thick, lumpy gel formed immediately. This was placed in a Pyrex liner in an autoclave and run eight days at 175° C. and autogenous pressure. A very hard product was removed, filtered, washed with 200 ml. H2 O, and dried at 230° F. Microscopic examination showed mainly large rod-shaped crystals to 8 × 20μ, some large cubes to 25μ. Reaction composition and product analysis are reported in Table 14.
TABLE 14
______________________________________
Reaction and product compositions
Example
26 27
______________________________________
Time, days 5 8
Temperature, ° C
175 175
Type .sup.(1) .sup.(2)
Reaction composition, moles:
SiO.sub.2 0.382 0.381
Al.sub.2 O.sub.3 0.0131 0.0131
[(C.sub.3 H.sub.8).sub.4 N].sub.2 O
0.118 0.118
H.sub.2 O 6.30 6.30
Na.sub.2 O 0.0159 0.1306
R.sub.4 N/(R.sub.4 N + Na)
0.881 0.644
SiO.sub.2 /Al.sub.2 O.sub.3
29.2 29.1
OH.sup.- /SiO.sub.2 0.618 0.619
H.sub.2 O/OH.sup.- 26.7 26.7
Product composition:
Na.sub.2 O, wt. percent
1.72 7.3
Al.sub.2 O.sub.3, wt. percent
4.0 8.3
SiO.sub.3, wt. percent
94.9 87.4
Total 100.62 103.0
SiO.sub.3 /Al.sub.2 O.sub.3
40.3 18.0
Na.sub.2 O/Al.sub.2 O.sub.3
0.71 1.42
Adsorption:
Cyclohexane, wt. percent
5.07
Normal hexane, wt. percent
10.15
Water, wt. percent 6.50
X-ray analysis ZSM-5 ZSM-5
______________________________________
.sup.1 TPA-OH plus Ludor.
.sup.2 TPABr plus NaOH.
Claims (13)
1. A process for converting a hydrocarbon charge which comprises contacting the same under hydrocarbon conversion conditions with a catalyst resulting from thermal treatment of a crystalline aluminosilicate zeolite having a composition in terms of mole ratios of oxides as follows:
0.9±0.2M.sub.2/n O:Al.sub.2 O.sub.3 :YSiO.sub.2 :zH.sub.2 O
wherein M is at least one cation having a valence n, Y is at least 5 and z is between 0 and 40, said thermally treated aluminosilicate catalyst having the X-ray diffraction lines of Table 1 of the specification.
2. The process of claim 1 wherein Y is 5-100.
3. The process of claim 1 wherein M comprises the cation selected from the group consisting of alkyl ammonium, metal, ammonium, hydrogen and mixtures thereof.
4. A process for cracking a hydrocarbon charge which comprises contacting the same under cracking conditions with a catalyst resulting from thermal treatment of a crystalline aluminosilicate zeolite having a composition in terms of mole ratios of oxides as follows:
0.9±0.2M.sub.2/n O:Al.sub.2 O.sub.3 :YSiO.sub.2 :zH.sub.2 O
wherein M is at least one cation having a valence n, Y is at least 5 and Z is between 0 and 40, said thermally treated aluminosilicate catalyst having the X-ray diffraction lines of Table 1 of the specification.
5. The process of claim 4 wherein Y is 5-100.
6. The process of claim 4 wherein M comprises the cation selected from the group consisting of alkyl ammonium, metal, ammonium, hydrogen and mixtures thereof.
7. A process for hydrocracking a hydrocarbon charge which comprises contacting the same in the presence of hydrogen under hydrocracking conditions with a catalyst resulting from thermal treatment of a crystalline aluminosilicate zeolite having a composition in terms of mole ratios of oxides as follows:
0.9±0.2M.sub.2/n O:Al.sub.2 O.sub.3 :YSiO.sub.2 :zH.sub.2 O
wherein M is at least one cation having a valence n, Y is at least 5 and z is between 0 and 40, said thermally treated aluminosilicate catalyst having the X-ray diffraction lines of Table 1 of the specification.
8. The process of claim 7 wherein Y is 5-100.
9. The process of claim 7 wherein M comprises the cation selected from the group consisting of alkyl ammonium, metal, ammonium, hydrogen, and mixtures thereof.
10. A process for isomerization of polyalkyl substituted aromatics which comprises contacting the same under isomerization conditions with a catalyst resulting from thermal treatment of a crystalline aluminosilicate zeolite having a composition in terms of mole ratios of oxides as follows:
0.9±0.2M.sub.2/n O:Al.sub.2 O.sub.3 :YSiO.sub.2 :zH.sub.2 O
wherein M is at least one cation having a valence n, Y is at least 5 and z is between 0 and 40, said thermally treated aluminosilicate catalyst having the X-ray diffraction lines of Table 1 of the specification.
11. The process of claim 10 wherein the polyalkyl substituted aromatic is ortho-xylene.
12. A process for the disproportionation of alkyl aromatics which comprises contacting the same under conversion conditions with a catalyst resulting from thermal treatment of a crystalline aluminosilicate zeolite having a composition in terms of mole ratios of oxides as follows:
0.9±0.2M.sub.2/n O:Al.sub.2 O.sub.3 :YSiO.sub.2 :zH.sub.2 O
wherein M is at least one cation having a valence n, Y is at least 5 and z is between 0 and 40, said thermally treated aluminosilicate catalyst having the X-ray diffraction lines of Table 1 of the specification.
13. The process of claim 12 wherein the alkyl aromatic is toluene. .Iadd. 14. The process of claim 7 wherein said hydrocracking conditions include a temperature between 400° F and 825° F, a pressure between 10 and 2500 p.s.i.g., a liquid hourly space velocity between 0.1 and 10 and a molar ratio of hydrogen to hydrocarbon between 2 and 80. .Iaddend..Iadd. 15. The process of claim 7 wherein said catalyst contains a hydrogenating component selected from the group consisting of tungsten, vanadium, molybdenum, rhenium, nickel, cobalt, chromium, manganese, platinum and palladium. .Iaddend..Iadd. 16. The process of claim 14 wherein said catalyst contains a hydrogenating component selected from the group consisting of tungsten, vanadium, molybdenum, rhenium, nickel, cobalt, chromium, manganese, platinum and palladium. .Iaddend.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US25479972A | 1972-05-18 | 1972-05-18 |
Related Parent Applications (3)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US630933A Continuation-In-Part US3390830A (en) | 1967-04-14 | 1967-04-14 | Sealing of horizontally-split centrifugal compressors |
| US86547269A Division | 1969-10-10 | 1969-10-10 | |
| US25479972A Reissue | 1969-10-10 | 1972-05-18 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| USRE29857E true USRE29857E (en) | 1978-12-05 |
Family
ID=22965632
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US05/866,576 Expired - Lifetime USRE29857E (en) | 1972-05-18 | 1978-01-03 | Conversion with ZSM-5 family of crystalline aluminosilicate zeolites |
Country Status (1)
| Country | Link |
|---|---|
| US (1) | USRE29857E (en) |
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| EP0018778A1 (en) * | 1979-04-27 | 1980-11-12 | Mobil Oil Corporation | Catalytic dewaxing of hydrocarbon oils |
| US4263129A (en) | 1979-09-04 | 1981-04-21 | Mobil Oil Corporation | Hydrotreating/hydrocracking process with low acidity catalyst |
| EP0040018A2 (en) * | 1980-05-12 | 1981-11-18 | Mobil Oil Corporation | Catalytic hydroconversion of residual stocks |
| US4518703A (en) | 1979-02-16 | 1985-05-21 | Union Oil Company Of California | Crystalline silica catalysts |
| US4560820A (en) | 1981-04-13 | 1985-12-24 | Chevron Research Company | Alkylaromatic dealkylation |
| US4676958A (en) | 1985-03-06 | 1987-06-30 | Chevron Research Company | Preparation of crystalline zeolites using magadiite |
| US4689207A (en) | 1985-03-06 | 1987-08-25 | Chevron Research Company | Process for the preparation of crystalline microporous organosilicates using magadiite as a silica source |
| US4899009A (en) | 1987-09-09 | 1990-02-06 | Nippon Petrochemicals Co. Ltd. | Method for producing m-benzyltolune |
| US4902841A (en) | 1987-03-11 | 1990-02-20 | Nippon Petrochemicals Company, Ltd. | Method for producing electrical insulating oil composition |
| US4982025A (en) * | 1988-03-09 | 1991-01-01 | Nippon Petrochemicals Company, Limited | Electrical insulating oil comprising improved fraction |
| US5877362A (en) * | 1996-09-12 | 1999-03-02 | Nippon Petrochemicals Company, Limited | Method for producing diphenylmethane |
| US5880322A (en) * | 1996-12-16 | 1999-03-09 | Nippen Petrochemicals Company, Limited | Method for producing diarylmethane |
| US6207866B1 (en) | 1997-07-11 | 2001-03-27 | Nippon Petrochemicals Company, Limited | Method for producing diarylmethane or its derivatives |
| US6300534B1 (en) | 1998-07-01 | 2001-10-09 | Nippon Petrochemicals Company, Limited | Process for producing dehydrogenated compounds of m-ethyldiphenylalkane |
| US6586362B1 (en) | 1999-09-20 | 2003-07-01 | Nippon Petrochemicals Company, Limited | Hydrocarbon solvent and pressure-sensitive copying material made with the same |
| US6660894B1 (en) * | 2000-11-21 | 2003-12-09 | Phillips Petroleum Company | Process for upgrading an oligomerization product |
| US20130085311A1 (en) * | 2011-09-29 | 2013-04-04 | Honam Petrochemical Corporation | Zsm-5 catalyst with micropores and mesopores, preparation method thereof and production method of light olefins through catalytic cracking of hydrocarbons using the catalyst |
| CN103028433A (en) * | 2011-09-29 | 2013-04-10 | 湖南石油化学株式会社 | ZSM-5 catalyst having micro-pore and meso pore, preparing method thereof and method of using the catalyst to conduct catalytic cracking on hydrocarbon to produce light olefins |
| US8877669B2 (en) | 2010-08-02 | 2014-11-04 | Basf Corporation | Hydroisomerization catalysts for biological feedstocks |
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| US3308069A (en) * | 1964-05-01 | 1967-03-07 | Mobil Oil Corp | Catalytic composition of a crystalline zeolite |
| US3248170A (en) * | 1965-04-08 | 1966-04-26 | Universal Oil Prod Co | Crystalline zeolite u |
| US3459676A (en) * | 1966-06-14 | 1969-08-05 | Mobil Oil Corp | Synthetic zeolite and method for preparing the same |
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| US4518703A (en) | 1979-02-16 | 1985-05-21 | Union Oil Company Of California | Crystalline silica catalysts |
| EP0018778A1 (en) * | 1979-04-27 | 1980-11-12 | Mobil Oil Corporation | Catalytic dewaxing of hydrocarbon oils |
| US4263129A (en) | 1979-09-04 | 1981-04-21 | Mobil Oil Corporation | Hydrotreating/hydrocracking process with low acidity catalyst |
| EP0040018A2 (en) * | 1980-05-12 | 1981-11-18 | Mobil Oil Corporation | Catalytic hydroconversion of residual stocks |
| EP0040018A3 (en) * | 1980-05-12 | 1981-12-16 | Mobil Oil Corporation | Catalytic hydroconversion of residual stocks |
| US4560820A (en) | 1981-04-13 | 1985-12-24 | Chevron Research Company | Alkylaromatic dealkylation |
| US4676958A (en) | 1985-03-06 | 1987-06-30 | Chevron Research Company | Preparation of crystalline zeolites using magadiite |
| US4689207A (en) | 1985-03-06 | 1987-08-25 | Chevron Research Company | Process for the preparation of crystalline microporous organosilicates using magadiite as a silica source |
| US4902841A (en) | 1987-03-11 | 1990-02-20 | Nippon Petrochemicals Company, Ltd. | Method for producing electrical insulating oil composition |
| US4899009A (en) | 1987-09-09 | 1990-02-06 | Nippon Petrochemicals Co. Ltd. | Method for producing m-benzyltolune |
| US4982025A (en) * | 1988-03-09 | 1991-01-01 | Nippon Petrochemicals Company, Limited | Electrical insulating oil comprising improved fraction |
| US5877362A (en) * | 1996-09-12 | 1999-03-02 | Nippon Petrochemicals Company, Limited | Method for producing diphenylmethane |
| US5880322A (en) * | 1996-12-16 | 1999-03-09 | Nippen Petrochemicals Company, Limited | Method for producing diarylmethane |
| US6207866B1 (en) | 1997-07-11 | 2001-03-27 | Nippon Petrochemicals Company, Limited | Method for producing diarylmethane or its derivatives |
| US6300534B1 (en) | 1998-07-01 | 2001-10-09 | Nippon Petrochemicals Company, Limited | Process for producing dehydrogenated compounds of m-ethyldiphenylalkane |
| US6586362B1 (en) | 1999-09-20 | 2003-07-01 | Nippon Petrochemicals Company, Limited | Hydrocarbon solvent and pressure-sensitive copying material made with the same |
| US6660894B1 (en) * | 2000-11-21 | 2003-12-09 | Phillips Petroleum Company | Process for upgrading an oligomerization product |
| US8877669B2 (en) | 2010-08-02 | 2014-11-04 | Basf Corporation | Hydroisomerization catalysts for biological feedstocks |
| US20130085311A1 (en) * | 2011-09-29 | 2013-04-04 | Honam Petrochemical Corporation | Zsm-5 catalyst with micropores and mesopores, preparation method thereof and production method of light olefins through catalytic cracking of hydrocarbons using the catalyst |
| CN103028433A (en) * | 2011-09-29 | 2013-04-10 | 湖南石油化学株式会社 | ZSM-5 catalyst having micro-pore and meso pore, preparing method thereof and method of using the catalyst to conduct catalytic cracking on hydrocarbon to produce light olefins |
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