A method of producing p-xylene comprising the steps of separating the reformate feed in the reformate splitter to produce a benzene stream, a combined heavy stream, a xylene stream, and a toluene stream, converting the C9+ aromatic hydrocarbons in the presence of a dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, separating the dealkylation effluent in the dealkylation splitter to produce a C9 stream and a C10+ stream, reacting the C9 stream, the toluene stream, the benzene stream, and the hydrogen stream in the presence of a transalkylation catalyst in the transalkylation reactor to produce a transalkylation effluent, separating the p-xylenes from the xylene stream in the p-xylene separation unit to produce a p-xylene product and a p-xylene depleted stream, converting the m-xylene and o-xylene in the p-xylene depleted stream in the isomerization unit to produce an isomerization effluent.

A catalytic cracking catalyst has a rare earth modified Y-type molecular sieve, an additive-containing alumina binder, and a clay. The rare earth modified Y-type molecular sieve has a rare earth oxide content of about 4-12 wt %, a phosphorus content of about 0-10 wt %, a sodium oxide content of no more than about 1.0 wt %, a total pore volume of about 0.36-0.48 mL/g, a percentage of the pore volume of secondary pores having a pore size of 2-100 nm to the total pore volume of about 20-40%, a lattice constant of about 2.440-2.455 nm, a percentage of non-framework aluminum content to the total aluminum content of no more than about 10%, a lattice collapse temperature of not lower than about 1060 C., and a ratio of B acid to L acid in the total acid content of the modified Y-type molecular sieve of no less than about 3.50.

A new aluminosilicate zeolite designated UZM-50, methods of making the zeolite, and its use as a catalyst in hydrocarbon conversion processes are described. This zeolite is represented by the empirical formula:
M.sup.+.sub.mR.sub.rAl.sub.1xE.sub.xSi.sub.yO.sub.z
where M is selected from the group consisting of hydrogen, sodium, potassium, magnesium, calcium or combinations thereof, R is the organic structure directing agent or agents derived from reactants R1 and R2 where R1 is an amine essentially incapable of undergoing pyramidal inversion and having 7 or fewer carbon atoms, and R2 is a dihaloalkane, and E is an element selected from the group consisting of gallium, iron, boron and mixtures thereof. UZM-50 has utility in various hydrocarbon conversion reactions such as conversion of an aromatic molecule to another aromatic molecule.

A catalyst, which comprises molecular sieves; a molecular sieve structure is at least provided with a one-dimension eight-membered annular small hole channel, wherein the diameter of a substance that may diffuse in the direction of the eight-membered annular channel is no less than 2.0 , and the diameter of a substance that may be accommodated in the molecular sieves is no more than 6 . The catalyst is used for a methanol- and/or dimethyl ether-to-propylene reaction, comprising causing methanol and/or dimethyl ether to make contact with a methanol-to-propylene catalyst to obtain propylene.

The present disclosure discloses a multistage nanoreactor catalyst and preparation and application thereof, belonging to the technical field of synthesis gas conversion. The catalyst consists of a core of an iron-based Fischer-Tropsch catalyst, a transition layer of a porous oxide or porous carbon material, and a shell layer of a molecular sieve having an aromatization function. The molecular sieve of the shell layer can be further modified by a metal element or a non-metal element, and the outer surface of the molecular sieve is further modified by a silicon-oxygen compound to adjust the acidic site on the outer surface and the aperture of the molecular sieve, thereby inhibiting the formation of heavy aromatic hydrocarbons. According to the disclosure, the shell layer molecular sieve with a transition layer and a shell layer containing or not containing auxiliaries, and with or without surface modification can be prepared by the iron-based Fischer-Tropsch catalyst through multiple steps. The catalyst can be used for direct preparation of aromatic compounds, especially light aromatic compounds, from synthesis gas; the selectivity of light aromatic hydrocarbons in hydrocarbons can be 75% or above, and the content in the liquid phase product is not less than 95%; and the catalyst has good stability and good industrial application prospect.

The invention relates to a multi-strand plant and a corresponding process for producing olefins from oxygenates in which a plurality of reactor trains which each comprise one or more catalyst-containing oxygenate-to-olefin (OTO) reaction zones are arranged in parallel and operated in parallel, wherein at least one of the parallel reaction zones may be operated in a regeneration mode while the OTO synthesis reaction may be performed in the other reaction zones parallel thereto. The partial product streams obtained from the individual reactor trains operated in a synthesis mode are discharged via partial product conduits, combined into a complete product conduit using a connecting device, compressed using a compressor and separated into a plurality of olefin-containing hydrocarbon fractions using a multi-stage workup apparatus. The inventive configuration of the plant and of the process reduces pressure drops and thus enhances the yield for short-chain olefins, for example propylene.

Process for the preparation of a catalyst and a catalyst comprising enhanced mesoporosity is provided herein. Thus, in one embodiment, provided is a particulate FCC catalyst comprising 2 to 50 wt % of one or more ultra stabilized high Si02/A1203 ratio large pore faujasite zeolite or a rare earth containing USY, 0 to 50 wt % of one or more rare-earth exchanged large pore faujasite zeolite, 0 to 30 wt % of small to medium pore size zeolites, 5 to 45 wt % quasi-crystalline boehmite 0 to 35 wt % microcrystalline boehmite, 0 to 25 wt % of a first silica, 2 to 30 wt % of a second silica, 0.1 to 10 wt % one or more rare earth components showiomg enhanced mesoporosity in the range of 6-40 nm, the numbering of the silica corresponding to their orders of introduction in the preparation process.

A reactor system for aromatization of higher hydrocarbons within a given temperature range T upon bringing a reactant stream including higher hydrocarbons into contact with a catalytic mixture. The reactor system includes a reactor unit arranged to accommodate a catalytic mixture. The catalytic mixture includes a catalyst material and a ferromagnetic material. The catalyst material is arranged to catalyze the aromatization of higher hydrocarbons. The ferromagnetic material is ferromagnetic at least at temperatures up to an upper limit of the given temperature range T, where the temperature range T is the range from between about 400 C. and about 700 C. or a subrange thereof. The reactor system also includes an induction coil arranged to be powered by a power source supplying alternating current, whereby the ferromagnetic material is heated to a temperature within the temperature range T by means of an alternating magnetic field.

Disclosed herein is a process for preparing a hydrocracking catalyst, comprising (i) combining a zeolite, a binder, water and a hydrogenating metal compound which is a complex or a salt of a hydrogenating metal to obtain a mixture, wherein the zeolite has not been treated with a phosphorus-containing compound and the zeolite has a silica to alumina molar ratio of 5-200; (ii) forming the mixture into a shaped body; and (iii) calcining the shaped body to form the catalyst.

A process is useful for the oligomerization of short-chain olefins in the presence of a catalyst, wherein the catalyst is kept in a dry atmosphere prior to being used in the process.