Disclosed is a catalyst comprising a zeolite comprising a framework, the framework comprising silicon and aluminum, and a noble metal. The zeolite has undergone at least a first exchange with a Group I or II cation or ammonium and thereafter is contacted with a second Group I or II cation. The step of contacting comprises an exchange, incipient wetness, or dry impregnation. The noble metal is deposited at the zeolite.

A process for producing valuable aromatic hydrocarbons from a crude or semi-crude shale gas stream. A crude or semi-crude shale gas stream including methane is introduced into a reactor that converts at least a portion of the ethane component into aromatic hydrocarbons. Unreacted methane, other hydrocarbons, and hydrogen may then be easily separated from the aromatic hydrocarbons. Because methane is not separated from the shale gas stream, the expensive and resource-consuming shale gas C1/C2+ separation step is avoided.

Disclosed are processes for conversion of a feedstock comprising C.sub.8+ aromatic hydrocarbons to lighter aromatic products in which the feedstock and optionally hydrogen are contacted in the presence of the catalyst composition under conversion conditions effective to dealkylate and transalkylate said C.sub.8+ aromatic hydrocarbons to produce said lighter aromatic products comprising benzene, toluene and xylene. The catalyst composition comprises a zeolite, a first metal, and a second metal, and is treated with a source of sulfur and/or a source of steam.

Disclosed are processes for rejuvenating catalysts comprising at least one Group 10 metal and a microporous crystalline metallosilicate, and hydrocarbon conversion processes including such rejuvenation processes. In an aspect, the rejuvenation process comprises contacting a deactivated catalyst comprising at least one Group 10 metal and a microporous crystalline metallosilicate with an oxygen-containing gaseous stream under conditions comprising a temperature ranging from about 250° C. to about 375° C. and a pressure of up to about 100 bar. In a further aspect, the rejuvenation process comprises contacting a deactivated catalyst comprising at least one Group 10 metal, at least one rare earth metal, and a microporous crystalline metallosilicate with an oxygen-containing gaseous stream under conditions comprising a temperature ranging from about 250° C. to about 500° C. and a pressure of up to about 100 bar.

Disclosed are a catalyst and a preparation method therefor, the catalyst being able to maintain a high production yield of C8 aromatic hydrocarbons in the process of converting a feedstock containing alkyl aromatics to C8 aromatic hydrocarbons such as mixed xylene through disproportionation/transalkylation/dealkylation while reducing a content of ethylbenzene in the products.

A process for producing isooctane by introducing a butane feed stream (containing n-butane, i-butane) and hydrogen into a catalytic hydrogenolysis reactor to produce a hydrogenolysis product stream; separating the hydrogenolysis product stream into a butane stream (i-butane, optionally n-butane); feeding the butane stream to a catalytic dehydrogenation reactor to produce a dehydrogenation product stream comprising saturated and unsaturated four-carbon hydrocarbons; and feeding the dehydrogenation product stream to an oligomerization unit to produce isooctene and dehydrogenating the isooctene to produce isooctane.

A process for preparing a catalyst composition comprising (a) preparing a carrier comprising (i) mordenite in an amount in the range of from 20 to 80 wt %, based on total weight of carrier, (ii) ZSM-5 type zeolite in an amount in the range of from 10 to 70 wt %, based on total weight of carrier; and (iii) an inorganic binder in an amount in the range of from 10 to 50 wt %, based on total weight of carrier; (b) incorporating in the carrier molybdenum in an amount in the range of from 1 to 10 wt %, as metal based on total weight of catalyst composition, and subjecting the thus treated carrier to a temperature of from 100 to at most 300 C. and (c) incorporating in the molybdenum containing carrier obtained in step (b) platinum in an amount of from 0.005 to 1 wt %, as metal based on total weight of catalyst composition, and subjecting the thus treated carrier to a temperature of from 200 to at most 600 C.; and a process for conversion of alkylaromatic hydrocarbons containing feedstock using a catalyst prepared by said process. Process using the prepared catalyst composition for alkylaromatic hydrocarbon conversion.

The present disclosure provides an aromatization catalyst, a preparation method, a regeneration method and an aromatization method thereof. The preparation method comprises steps of: mixing a zeolite molecular sieve with a binder to obtain a catalyst precursor; the catalyst precursor is successively subjected to an ion exchange modification and a first modification treatment, and then subjected to a hydrothermal treatment, and further subjected to active metal loading and a second modification treatment, to obtain the aromatization catalyst. The aromatization catalyst has good carbon deposition resistance and high aromatization activity, and enables an aromatization reaction to be completed under mild conditions, and has high aromatic selectivity, and the liquid yield is above 98.5%.

The present discloses an aromatization catalyst, preparation process and application thereof and a low-carbon olefin aromatization process. The aromatization catalyst comprises a microporous material, a binder and a modifier; the microporous material is a zeolite molecular sieve, the binder is alumina, the modifier is phosphorus, and the molar ratio of the aluminum element in the binder to the phosphorus element is more than or equal to 1 and less than 5; the ratio of the acidity of the strongly acidic sites to the acidity of the weakly acidic sites of the olefin aromatization catalyst is less than 1.

Catalyst compositions comprising an inorganic porous material with pore diameters of at least 2 nm and of crystals of molecular sieve, characterized in that the crystals of molecular sieve have an average diameter, measured by scanning electron microscopy, not bigger than 50 nm, and in that the catalyst composition presents a concentration of acid sites ranges from 50 to 1200 mol/g measured by TPD NH3 adsorption; and the XRD pattern of said catalyst composition is the same as the X ray diffraction pattern of said inorganic porous material.