Methods of catalytic hydrogenation, including methods that may be used to hydrogenate an unsaturated reactant to produce an at least partially saturated product that may be a solid at 20° C. Systems for catalytic hydrogenation that may include a reactor bed containing one or more activated carbon monolith catalysts. At least 97% of unsaturated bonds may be saturated by the methods and systems.

The chemical conversion of renewable oil to obtain a hydrocarbon product suitable as a fuel, includes (i) renewable oil including corn distillers oil (CDO), fatty acid glyceryl esters (FAGE), triacylglycerols (TAG), lipids, and free fatty acids (FFA), which are derived from non-fossil-fuel sources that include animals, plants, vegetables, fruits, grains, algae, and plankton (collectively “oil”); (ii) the chemical transformation of the oil by substantially reducing or eliminating the carboxylate functionality and native unsaturations of fatty acids contained therein; (iii) wherein the hydrocarbon product is substantially a mixture of saturated hydrocarbons, or alkanes, originating from corresponding structures in the oil, e.g., the hydrocarbon chains of fatty acids; and (iv) the product mixture is suitable as fuel that may be blended with or be used in place of fuel such as diesel derived from petroleum.

Methods of catalytic hydrogenation, including methods that may be used to hydrogenate an unsaturated reactant to produce an at least partially saturated product that may be a solid at 20° C. Systems for catalytic hydrogenation that may include a reactor bed containing one or more activated carbon monolith catalysts. At least 97% of unsaturated bonds may be saturated by the methods and systems.

A method of making alkanes from lignocellulosic sources of C5 and C6 sugars. Suitable biomass feedstocks are converted into alkane-based fuels such as diesel and jet fuel blendstocks. Sugar monomers from the feedstocks are converted to chloromethylfurfural (CMF) with a levulinic acid (LA) byproduct. The CMF and LA are converted to ethyl levulinate (EL) and hydroxymethylfurfural (HMF), which are then combined into longer chain molecules via aldol condensation reactions. The condensation products are partially or fully saturated by mild hydrotreating, followed by deoxygenation to form alkanes with boiling ranges suitable for use as liquid fuels.

Catalyst compositions including a zeolite having a molar ratio of silicon to aluminum of about 10.0 to about 300.0; a Group 10-12 element and combinations thereof; a Group 15 element and combinations thereof; and optionally, a binder, wherein the catalyst composition has a molar ratio of Group 15 element to Group 10-12 element of about 0.01 to about 10.0 are disclosed. Methods of converting organic compounds to aromatics using such catalyst compositions are also disclosed.

A catalyst composition includes a zeolite, a binder, and a Group 12 transition metal selected from the group consisting of Zn, Cd, or a combination thereof, the zeolite having a silicon to aluminum ratio of at least about 10, the catalyst composition comprising about 50 wt % or less of the binder based on a total weight of the catalyst composition, the catalyst composition having a micropore surface area of at least about 340 m.sup.2/g, a molar ratio of Group 12 transition metal to aluminum of about 0.1 to about 1.3, and at least one of (a) a mesoporosity of greater than about 20 m.sup.2/g; (b) a diffusivity for 2,2-dimethylbutane of greater than about 110.sup.2 sec.sup.1 when measured at a temperature of about 120 C. and a 2,2-dimethylbutane pressure of about 60 torr (about 8 kPa).

A catalyst composition comprising a zeolite, an alumina binder, and a Group 12 transition metal selected from Zn and/or Cd, the zeolite having a Si/Al ratio of at least about 10 and a micropore surface area of at least about 340 m.sup.2/g, the catalyst composition comprising about 50 wt % or less of the binder, based on a total weight of the catalyst composition, and having a micropore surface area of at least about 290 m.sup.2/g, a molar ratio of Group 12 transition metal to aluminum of about 0.1 to about 1.3, and at least one of: a mesoporosity of about 20 m.sup.2/g to about 120 m.sup.2/g; a diffusivity for 2,2-dimethylbutane of greater than about 110.sup.2 sec.sup.1 when measured at a temperature of about 120 C. and a 2,2-dimethylbutane pressure of about 60 torr (8 kPa); and a combined micropore surface area and mesoporosity of at least about 380 m.sup.2/g.

A catalyst composition comprises a self-bound zeolite and a Group 12 transition metal selected from the group consisting of Zn, Cd, or a combination thereof, the zeolite having a silicon to aluminum ratio of at least about 10, the catalyst composition having a micropore surface area of at least about 340 m.sup.2/g, a molar ratio of Group 12 transition metal to aluminum of about 0.1 to about 1.3, and at least one of: (a) a mesoporosity of greater than about 20 m.sup.2/g; (b) a diffusivity for 2,2-dimethylbutane of greater than about 1?10.sup.?2 sec.sup.?1 when measured at a temperature of about 120? C. and a 2,2-dimethylbutane pressure of about 60 torr (about 8 kPa).

In an embodiment, a hydrocarbon cracking process for converting a mixed hydrocarbon feedstock to olefins is disclosed. The hydrocarbon cracking process includes: a) catalytically cracking the mixed hydrocarbon feedstock comprising renewable/circular feedstock within a fluid catalytic cracker (FCC) by contacting the mixed hydrocarbon feedstock under suitable catalytic cracking conditions with a fluidized cracking catalyst to produce at least a catalytically cracked gas product; b) separating the catalytically cracked gas product in a separator to produce an ethane product and ethylene; c) steam cracking the ethane product to produce a light steam cracked product; and d) recycling the light steam cracked product to the separator in step b) to produce a portion of the ethylene.