The invention relates to treating a molecular sieve prepared by at least one in situ selectivation sequence wherein graphitic coke is adhered to said molecular sieve, which is useful in a toluene disproportionation process.

The present disclosure relates to a method for upgrading hydrocarbon using C4, C5 and C6 streams, and more specifically, to a method for upgrading hydrocarbons using C4, C5 and C6 streams. The method includes the steps of: preparing C4, C5 and C6 streams, which are the products of naphtha catalytic cracking (NCC) process, heavy oil upgrading process, thermal cracking process, or fluidized catalytic cracking (FCC or RFCC) process; oligomerizing the C4, C5 and C6 streams with a catalyst to produce branched unsaturated hydrocarbons; and fractional distillating the branched unsaturated hydrocarbons to separate into C14-18 products or C32-40 products.

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.

Provided here are systems and methods that integrate a hydrodearylation process and a transalkylation process into an aromatic recovery complex. Various other embodiments may be disclosed and claimed.

According to one or more embodiments of the present disclosure, chemical streams may be processed by a method which may comprise operating a first chemical process, stopping the first chemical process and removing the first catalyst from the reactor, and operating a second chemical process. The reaction of the first chemical process may be a dehydrogenation reaction, a cracking reaction, a dehydration reaction, or a methanol-to-olefin reaction. The reaction of the second chemical process may be a dehydrogenation reaction, a cracking reaction, a dehydration reaction, or a methanol-to-olefin reaction. The first reaction and the second reaction may be different types of reactions.

A method for converting shale gas to aromatic hydrocarbons includes passing a feedstock comprising ethane gas and methane gas to an aromatization reactor; converting a portion of the methane gas and ethane gas in the feedstock to liquid aromatic hydrocarbons with a zeolite based catalyst at a temperature of 750 C to 900 C; separating unconverted methane gas from liquid aromatic hydrocarbons; separating unconverted methane gas from the unconverted ethane gas; recycling the separated methane gas to the aromatization reactor; recovering aromatic hydrocarbons in a product stream after separation and removal from the aromatization reactor. Less than or equal to 95% of the ethane is converted to aromatic hydrocarbons.

Process for the preparation of a catalyst and a catalyst comprising the use of more than one silica source is provided herein. Thus, in one embodiment, the invention provides a particulate FCC catalyst comprising about 5 to about 60 wt % one or more zeolites, about 15 to about 35 wt % quasicrystalline boehmite (QCB), about 0 to about 35 wt % microcrystalline boehmite (MCB), greater than about 0 to about 15 wt % silica from sodium stabilized basic colloidal silica, greater than about 0 to about 30 wt % silica from acidic colloidal silica or polysilicic acid, and the balance clay and the process for making the same. This process results in attrition resistant catalysts with a good accessibility.

Processes for producing two or more different C.sub.2-C.sub.6 linear or branched olefins are disclosed herein. In one exemplary implementation, the process can include contacting a first feed stream that includes -valerolactone with one or more first catalysts in a first reactor to form a mixture. The mixture includes two or more different C.sub.2-C.sub.6 linear or branched olefins at a yield of at least 60%, and the one or more first catalysts include a doped zeolite. Processes for converting levulinic acid to -valerolactone are also disclosed herein.

Depolymerization processes and systems for converting polyolefin waste and other waste plastic to hydrocarbons, specifically liquid and gaseous depolymerization reaction products. A depolymerization or catalytic pyrolysis process can be conducted on a process feed which includes a polyolefin waste and a hydrocarbon co-feed under depolymerization conditions, including contacting the reactor feed with a depolymerization catalyst such as a zeolite-based catalyst. The resulting reactor effluent subsequently can be used as feeds or co-feeds for making circular products such as circular ethylene and circular polyethylene.

In a process and system for treatment of feed stocks comprising alkylating agent and metal salts, the metal salts are removed from the feedstock by an efficient combination of separations processes. The processes may take place in one or more stages, each stage taking place in one or more vessels. Such treatment processes may remove 99.9% or more of metal salts from a feedstock, while recovering 99.9% or more of the alkylating agent from the feedstock for use in an alkylation reaction, especially of aromatics such as toluene and benzene. Preferred alkylating agents include methanol and mixtures of carbon monoxide and hydrogen, for methylation of toluene and/or benzene. The methylation proceeds over an aluminosilicate catalyst and preferably yields para-xylene with 75% or greater selectivity.