Abstract: There is provided a process for converting methanol and/or dimethyl ether to a product containing C2 to C4 olefins which comprises the step of contacting a feed which contains methanol and/or dimethyl ether with a catalyst comprising a porous crystalline material. The contacting is conducted in the presence of a cofed aromatic compound under conversion conditions including a temperature of about 350° C. to about 550° C. and a methanol and/or dimethyl ether partial pressure less than or equal to 50 psia (345 kPa). The porous crystalline material used in the catalyst has a pore size greater than the critical diameter of the aromatic compound and a Diffusion Parameter for 2,2-dimethylbutane of about 0.1 to about 26 sec−1 when measured at a temperature of 120° C. and a 2,2- dimethylbutane pressure of 60 torr (8 kPa), and the aromatic compound is capable of alkylation by the methanol and/or dimethyl ether under said conversion conditions.

Abstract: There is provided a process for converting methanol and/or dimethyl ether to a product containing olefin, e.g., C2 to C4 olefins, C9+ aromatics and non-C9+ aromatics which comprises: 1) contacting a feed which contains methanol and/or dimethyl ether with a catalyst comprising a porous crystalline material, said contacting step being conducted in the presence of aromatics comprising C9 or C9+ aromatic compound produced in said process under conversion conditions including a temperature of 350° C. to 480° C. and a methanol partial pressure in excess of 10 psia (70 kPa), said porous crystalline material having a Diffusion Parameter for 2,2-dimethylbutane of about 0.1 sec−1 to about 20 sec−1 when measured at a temperature of 120° C.

Abstract: There is provided a process for the selective production of para-xylene which comprises reacting toluene with methanol in the presence of a catalyst comprising a porous crystalline material having a Diffusion Parameter for 2,2 dimethylbutane of about 0.1-15 sec−1 when measured at a temperature of 120° C. and a 2,2 dimethylbutane pressure of 60 torr (8 kPa). The porous crystalline material is preferably a medium-pore zeolite, particularly ZSM-5, which has been severely steamed at a temperature of at least 950° C. The porous crystalline material is preferably combined with at least one oxide modifier, preferably including phosphorus, to control reduction of the micropore volume of the material during the steaming step.

Abstract: There is provided a process for the selective production of para-xylene which comprises reacting toluene with methanol in the presence of a catalyst comprising a porous crystalline material having a Diffusion Parameter for 2,2 dimethylbutane of about 0.1-15 sec−1 when measured at a temperature of 120° C. and a 2,2 dimethylbutane pressure of 60 torr (8 kPa). The porous crystalline material is preferably a medium-pore zeolite, particularly ZSM-5, which has been severely steamed at a temperature of at least 950° C. The porous crystalline material is preferably combined with at least one oxide modifier, preferably including phosphorus, to control reduction of the micropore volume of the material during the steaming step.

Abstract: There is provided a process for the selective production of para-xylene which comprises reacting toluene with methanol in the presence of a catalyst comprising a porous crystalline material having a Diffusion Parameter for 2,2 dimethylbutane of about 0.1-15 sec−1 when measured at a temperature of 120° C. and a 2,2 dimethylbutane pressure of 60 torr (8 kPa). The porous crystalline material is preferably a medium-pore zeolite, particularly ZSM-5, which has been severely steamed at a temperature of at least 950° C. The porous crystalline material is preferably combined with at least one oxide modifier, preferably including phosphorus, to control reduction of the micropore volume of the material during the steaming step.

Abstract: A C4+naphtha hydrocarbon feed is converted to light olefins and aromatics, by contacting the feed with a catalyst containing ZSM-5 and/or ZSM-11, a substantially inert matrix material such as silica and/or clay, having less than about 20 wt % active matrix material based on total catalyst composition, and phosphorus.

Abstract: A hydrocarbon feed containing C4-C7 olefins and/or paraffins is converted to light olefins, by contacting the feed with a catalyst containing ZSM-5 and/or ZSM-11, having an initial silica to alumina ratio greater than about 300:1, and phosphorus.

Abstract: Para-xylene is produced by toluene methylation by charging toluene and a methylating agent to a fluidized bed of catalyst at a rate sufficient to maintain the fluidized bed in a turbulent sub-transport flow regime, reacting the toluene with the methylating agent, and recovering para-xylene from the fluidized bed. The fluidizable catalyst is a microporous material having a Constraint Index of about 1 to about 12. The relative concentration of the catalyst particles having a major dimension of less than 40 microns is controlled at between about 5 and 35 weight percent. The catalyst particles have an apparent particle density of about 0.9 to 1.6 grams per cubic centimeter, a size range of about 1 to 150 microns, and average particle size of about 20 to 100 microns.

Abstract: A process is disclosed for alkylating an isoparaffin with an olefin comprising the steps of:(a) reacting an isoparaffin having from 4 to 8 carbon atoms with an olefin having from 2 to 12 carbon atoms in a first alkylation reaction stage at temperature from about -40.degree. C. to about 500.degree. C. and overall isoparaffin:olefin feed weight ratio of from about 1:1 to about 250:1 with a solid alkylation catalyst comprising a synthetic porous crystalline material characterized by an X-ray diffraction pattern including values substantially as set forth in Table I of the specification and having a composition comprising the molar relationshipX.sub.2 O.sub.3 :(n)YO.sub.

Abstract: There is provided a process and a catalyst for hydrocracking hydrocarbons, such as gas oils. The catalyst comprises a hydrogenating metal and small crystal size zeolite Y. The zeolite Y may have a crystal size of less than one micron. Examples of hydrogenating metals include nickel and tungsten.

Abstract: There is provided a method for preparing an alumina bound, zeolite catalyst, wherein a zeolite of low silanol content is used as the source of zeolite used to prepare the catalyst. A particular zeolite used in this catalyst is zeolite Y. This catalyst may be combined with at least one hydrogenation component and used to hydrocrack hydrocarbons, such as gas oils. In particular, an NiW/USY/alumina catalyst may be used in a hydrocracking reaction to produce distillate boiling range hydrocarbons from higher boiling hydrocarbons.

Abstract: A benzene-rich gasoline stream is alkylated with higher olefins in contact with a fluid bed of shape selective zeolite catalyst to produce a gasoline product stream reduced in benzene content wherein the high octane value alkylaromatics formed by benzene alkylation are of low carbon number, essentially C10-. Concurrently, a portion of olefins in the gasoline stream are converted to gasoline boiling range hydrocarbons and the sulfur content of the gasoline feedstream is lowered. Besides enhancing the octane value of the feedstream, the process results in a lower Reid vapor pressure and lower sulfur content.

Abstract: A process is disclosed for producing alkyl tertiary alkyl ether such as TAME from alkanol and hydrocarbon feedstock containing linear olefins, iso-olefins, linear alkanes and iso-alkanes such as C5 streams from FCC. The process selectively etherifies iso-olefins in a plural stage etherification zone whose linear olefin-containing effluent is treated by distillation to remove iso-alkanes, and alkanol before passing to a skeletal isomerization zone using constrained intermediate pore size zeolite catalyst such as ZSM-22, ZSM-23, or ZSM-35, which converts linear olefins to iso-olefins which are cycled for etherification. The use of distillation to remove iso-alkanes and alkanol reduces mass flow to the etherification process and minimizes skeletal isomerization catalyst poisoning by alkanol, without resort to water extraction processes which require subsequent treatment of the isomerization zone feed to remove water.

Abstract: A process for upgrading low octane naphthas to produce gasoline products with low levels of benzene and aromatics while retaining a high pool octane uses a paraffinic naphtha reformer feed which is dehexanized to provide a C.sub.7 + fraction which is fed to the reformer and a C.sub.6 fraction which is fed together with the C.sub.6 fraction from the reformer effluent to a catalytic upgrading step where the low octane components from the naphtha and the benzene from the reformate are converted to a low benzene, high octane gasoline by alkylation of the benzene and other aromatics present in the reformate. The process has the advantage that benzene make in the reformer is reduced by the partial by-passing of the C.sub.6 benzene precursors around the reformer; in addition, improved benzene alkylation results from the presence of additional light olefins generated by the cracking of paraffins from the paraffinic naphtha. the reaction is preferably carried out in a turbulent fluidized bed reaction zone.

Abstract: An olefin hydration catalyst is regenerated with a non-oxidizing light gas, such as hydrogen. Light olefins, especially propylene, are converted to a mixture of alcohol(s), such as isopropanol (IPA) and ether(s), such as diisopropylether (DIPE) by contacting a feed containing the olefin with water and/or alcohol with the olefin hydration catalyst. Regeneration conditions include temperatures of from about 150.degree. C. to about 550.degree. C., pressures below about 1000 psig (6900 kPa). Lower pressures of regeneration unexpectedly demonstrated more effective catalyst regeneration through greater coke removal.

Abstract: There is provided a process and a catalyst for hydrocracking hydrocarbons, such as gas oils. The catalyst comprises a hydrogenating metal and small crystal size zeolite Y. The zeolite Y may have a crystal size of less than one micron. Examples of hydrogenating metals include nickel and tungsten.

Abstract: A continuous process for upgrading reformate feedstock or the like to reduce benzene content and increase octane fuel rating. The improved process comprises maintaining a fluidized bed of regenerable acid solid medium pore zeolite catalyst particles in a turbulent regime reaction zone, preferably maintained with a superficial gas velocity of 0.1 to 1 meter/sec. with reformate feedstock being introduced at a bottom portion of the reaction zone at a weight hourly space velocity (WHSV) of 0.1 to 5, based on active catalyst solids; reaction zone total pressure being less than 2000 kPa. The preferred catalyst particles have an average particle size of 20 to 100 microns (.mu.), with about 10 to 25% of the catalyst particles comprising fine particles having a particle size less than 30 microns; and the preferred zeolite catalyst comprises shape selective medium pore aluminosilicate zeolite having a constraint index of 1 to 12. The benzene is reacted by contacting reformate feedstock, such as C.sub.

Abstract: A method for conversion of linear C5 olefins in the presence of contaminant diolefins to corresponding iso-olefins of the same carbon number which comprises contacting a linear C5 olefin-containing organic feedstock with a catalyst comprising material having the structure of ZSM-35 under skeletal isomerization conditions, wherein said conversion is carried out at temperatures between about 100.degree. and 750.degree. C., weight hourly space velocities (WHSV) based on linear C5 olefins in said feedstock between 0.1 and 500 WHSV, C5 linear olefin partial pressures between 2 and 2000 kPa, and in the presence of hydrogen added in an amount sufficient to enhance linear C5 olefin conversion activity and extend the catalyst life of the catalyst relative to operation without any hydrogen added.

Abstract: There is provided a method for preparing an alumina bound, zeolite catalyst, wherein a zeolite of low silanol content is used as the source of zeolite used to prepare the catalyst. A particular zeolite used in this catalyst is zeolite Y. This catalyst may be combined with at least one hydrogenation component and used to hydrocrack hydrocarbons, such as gas oils. In particular, an NiW/USY/alumina catalyst may be used in a hydrocracking reaction to produce distillate boiling range hydrocarbons from higher boiling hydrocarbons.

Abstract: A method for starting up a fixed bed propylene hydration reactor containing shape selective metallosilicate catalyst particles for the production of isopropanol and/or diisopropyl ether is disclosed comprising the following sequential steps: contacting a feedstream comprising propane with catalyst particles in a hydration reactor; then introducing a feedstream comprising isopropanol into the reactor to displace propane. Next, a feedstream comprising propylene is introduced into the reactor under etherification conditions. Finally, a feedstream is introduced in the reactor comprising water under etherification and hydration reaction conditions whereby diisopropyl ether and isopropanol are produced.