The present invention relates to a catalyst for producing light olefins from catalytic cracking of hydrocarbon having 4 to 7 carbon atoms, wherein said catalyst comprises zeolite having the ring arrangement of 8 to 10 silicon atoms and hierarchical zeolite comprising 0.1 to 2 nm of micropore, 2 to 50 nm of mesopore, and greater than 50 nm of macropore, wherein the mesopore and macropore are greater than or equal to 40% when comparing to total pore volume, and said catalyst comprises element having 2.sup.+ to 4.sup.+ oxidation state with 0.1 to 3% by weight of the catalyst.

A process for preparing C2 to C3 hydrocarbons may include introducing a feed stream including hydrogen gas and a carbon-containing gas comprising carbon monoxide, carbon dioxide, and mixtures thereof into a reaction zone of a reactor, and converting the feed stream into a product stream comprising C2 to C3 hydrocarbons in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst may include a metal oxide catalyst component and a microporous catalyst component comprising 8-MR pore openings less than or equal to 5.1 A and a cage defining ring size less than or equal to 7.45 A, where a C2/C3 carbon molar ratio of the product stream is greater than or equal to 0.7.

Systems and methods are provided for integrated conversion of biomass to ultimately form naphtha and/or diesel boiling range products. The integrated conversion can include an initial conversion of biomass to alcohols, such as by fermentation, followed by conversion of alcohols to olefins and then olefins to naphtha, jet, and diesel boiling range compounds, with high selectivity for formation of diesel boiling range compounds. The integrated conversion process can be facilitated by using a common catalyst for both the conversion of alcohols to olefins and the conversion of olefins to naphtha and/or diesel boiling range compounds. For example, ZSM-48 (an MRE zeotype framework structure catalyst) can be used as the catalyst for both conversion of alcohols to olefins and for oligomerization of olefins with increased selectivity for formation of diesel boiling range products.

A process for producing olefins from the hydrocarbon feed includes introducing the hydrocarbon feed into a Solvent Deasphalting Unit (SDA) to remove asphaltene from the hydrocarbon feed producing a deasphalted oil stream, wherein the SDA comprises a solvent that reacts with the hydrocarbon feed, and the deasphalted oil stream comprises from 0.01 weight percent (wt. %) to 18 wt. % asphaltenes; introducing the deasphalted oil stream into a steam catalytic cracking system; steam catalytically cracking the deasphalted oil stream in the steam catalytic cracking system in the presence of steam and a nano zeolite cracking catalyst to produce a steam catalytic cracking effluent; and separating the olefins from the steam catalytic cracking effluent.

The present disclosure is directed to microporous crystalline aluminosilicate structures with GME topologies having pores containing organic structure directing agents (OSDAs) comprising at least one piperidinium cation, the compositions useful for making these structures, and methods of using these structures. In some embodiments, the crystalline zeolite structures have a molar ratio of Si:Al that is greater than 3.5.

A process for the production of an aromatic compound which comprise reacting a mixture comprising ethylene and a furan compound over a zeolitic material having a BEA-type framework structure is described, wherein the zeolitic material having a BEA-type framework structure comprised in the catalyst is obtainable and/or obtained according to an organotemplate-free synthetic process.

The present disclosure relates to a process for converting one or more methyl halides to acyclic C3-C6 olefins, said process comprising the steps of (a) providing a feedstream comprising one or more methyl halides; (b) providing a catalyst composition; and (c) contacting said feedstream with said catalyst composition under reaction conditions. The process is remarkable in that said reaction conditions include a reaction temperature below 400° C., and in that said catalyst composition comprises one or more molecular sieves with a Si/Al atomic ratio ranging from 2 to 18 and wherein said one or more molecular sieves comprise a plurality of pores, wherein said pores have a shape of an 8-membered ring or less.

This disclosure provides an improved process for converting benzene/toluene via methylation with methanol/dimethyl ether for producing, e.g., p-xylene, comprising separating and recycling dimethyl ether from the methylation reaction product mixture effluent to the methylation reactor. High selectivity toward p-xylene, among others, can be achieved.

Molecular sieves comprising intergrowths of cha and aft having an “sfw-GME tail”, at least one structure directing agent (SDA) within the framework of the molecular sieve, an intergrowth of CHA and GME framework structures, cha cavities, and aft cavities are described. A first SDA comprising either an N,N-dimethyl-3,5-dimethylpiperidinium cation or a N,N-diethyl-2,6-dimethylpiperidinium cation is required. A second SDA, which can further be present, is a CHA or an SFW generating cation. The amount of the second SDA-2 used can change the proportion of the components in the cha-aft-“sfw-GME tail”. Activated molecular sieves formed from SDA containing molecular sieves are also described. Compositions for preparing these molecular sieves are described. Methods of preparing a SDA containing JMZ-11, an activated JMZ-11, and metal containing activated JMZ-11 are described. Methods of using activated JMZ-11 and metal containing activated JMZ-11 in a variety of processes, such as treating exhaust gases and converting methanol to olefins are described.

The present disclosure concerns a process for converting methyl halides to ethylene and propylene, said process comprising the steps of (a) providing a feedstream comprising methyl halides; (b) providing a first and second catalyst composition, said second catalyst composition comprising a cracking catalyst; (c) contacting said feedstream with said first catalyst composition in a first reaction zone under first reaction conditions to provide a first product stream; and (d) subjecting at least a part of said first product stream to an Olefin Catalytic Cracking with said second catalyst composition in a second reaction zone under second reaction conditions to provide a second product steam. The process is remarkable in that said step (c) is performed under 400° C., and in that said first catalyst composition comprises molecular sieves with a Si/Al atomic between 2 and 18 and with a plurality of pores with a shape of an 8-membered ring or less.