Forming a diene includes contacting a reactant including at least one of a cyclic ether and a diol with a heterogeneous acid catalyst to yield a reaction mixture including a diene. The heterogeneous acid catalyst includes at least one of a Lewis acid catalyst, a supported Lewis-acid catalyst, a Brnsted acid catalyst, a solid acid catalyst, a supported phosphoric acid catalyst, and a sulfonated catalyst. The dehydration of cyclic ethers and diols with high selectivity to yield dienes completes pathways for the production of dienes, such as isoprene and butadiene, from biomass in high yields, thereby promoting economical production of dienes from renewable resources.

This present disclosure relates to catalytic processes for upgrading crude and/or refined fusel oil mixtures to higher value renewable chemicals, via mixed metal oxide or zeolite catalysts. Disclosed herein are processes passing a vaporized stream of crude and/or refined fusel oils over various mixed metal oxide catalysts, metal doped zeolites, or non-metal doped zeolites and/or metal oxides providing options to valorize fusel oil mixtures to higher value products. Renewable chemicals formed, via these upgrading catalyst platforms, are comprised of, but not limited to, methyl isobutyl ketone (MIBK), di-isobutyl ketone (DIBK), isoamylene, and isoprene.

The present disclosure provides methods to produce para-xylene, toluene, and other compounds from renewable sources (e.g., cellulose, hemicellulose, starch, sugar) and ethylene in the presence of a catalyst. For example, cellulose and/or hemicellulose may be converted into 2,5-dimethylfuran (DMF), which may be converted into para-xylene by cycloaddition of ethylene to DMF. Para-xylene can then be oxidized to form terephthalic acid.

Processes for transalkylation of aromatic hydrocarbons is disclosed. The process includes introducing a feed stream comprising aromatic hydrocarbon compounds to a transalkylation zone. A water source is introduced to the transalkylation zone, the water source being in an amount to provide about 80 to about 120 wppm of water based upon the mass of the feed stream. The feed stream is contacted with a transalkylation catalyst in the transalkylation zone under transalkylation conditions comprising a transalkylation temperature of about 130 C. to about 230 C. in the presence of the water to provide a transalkylation reaction effluent.

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 SiO2/Al2O3 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.

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 transalkylation of aromatic hydrocarbons is disclosed. The process includes introducing a feed stream comprising aromatic hydrocarbon compounds to a transalkylation zone. A water source is introduced to the transalkylation zone, the water source being in an amount to provide about 80 to about 120 wppm of water based upon the mass of the feed stream. The feed stream is contacted with a transalkylation catalyst in the transalkylation zone under transalkylation conditions comprising a transalkylation temperature of about 130 C. to about 230 C. in the presence of the water to provide a transalkylation reaction effluent.

The invention relates to a process for the catalytic cracking of a gasoline feedstock for the production of light olefins, in which said gasoline feedstock is brought into contact with a catalyst comprising at least one zeolite NU-86, alone or in a mixture with at least one other zeolite, at a temperature comprised between 500 and 700 C., at an absolute pressure comprised between 10 and 60 MPa, and with a contact time of the feedstock on said catalyst comprised between 10 milliseconds and 100 seconds.

Provided herein are methods for producing cyclic and acyclic ketones from trimerization and dimerization of alkyl ketones, including for example methyl ketones. Such cyclic and acyclic ketones may be suitable for use as fuel and lubricant precursors, and may be hydrodeoxygenated to form their corresponding cycloalkanes and alkanes. Such cycloalkanes and alkanes may be suitable for use as fuels, including jet fuels, and lubricants.

Process for the preparation of a catalyst by adding, clay, boehmite, a first silica to form a slurry, digesting the slurry with a monoprotic acid to a pH of less than 4, adding one or more zeolites, adding a rare earth component to the slurry and mixing, adjusting the slurry pH to below 4 with monoprotic acid, adding a second silica anywhere in the preceding steps, destabilizing the slurry by raising the pH, shaping and collecting the resulting catalyst, wherein the resulting catalyst has enhanced mesoporosity.