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.

The present invention provides a composition comprising 10-40 mass! of C.sub.8-30 linear alkanes, up to 20 mass % of C.sub.7-20 aromatic hydrocarbons, at least 90 mass % of which are monoaromatic, and no more than 1 massl in total of oxygen containing compounds; wherein the total amount of C.sub.8-30 alkanes in the composition is 50-95 mass % (and the total amount of C.sub.8-30 alkanes, C.sub.7-20 aromatic hydrocarbons and C.sub.8-30 cycloalkanes is at least 95 massl; and wherein the amounts are based on the mass of the composition. Also provided is a method for producing the composition comprising the step of hydroprocessing a biological feedstock using a catalyst and the step of fractionating the product of the hydroprocessing step.

A process for producing liquid hydrocarbon products from a biomass-containing feedstock and/or a biomass-derived feedstock is provided. The process comprises:

a) contacting the feedstock with a hydropyrolysis catalyst composition and molecular hydrogen in a hydropyrolysis reactor vessel to produce a product stream comprising a deoxygenated hydrocarbon product, H.sub.2O, H.sub.2, CO.sub.2, CO, C.sub.1-C.sub.3 gases, char and catalyst fines;

b) removing char and catalyst fines from said product stream;

c) cooling the remaining product stream to a temperature of no more than 300? C.; and

d) hydroconverting all or a portion of said deoxygenated hydrocarbon product in a hydroconversion reactor in the presence of one or more catalyst compositions suitable for the aromatic saturation of the deoxygenated hydrocarbon product and of the H.sub.2O, CO.sub.2, CO, H.sub.2, and C.sub.1-C.sub.3 gas generated in step a), to produce a product comprising C.sub.4+ hydrocarbon product, H.sub.2O, CO, CO.sub.2, and C.sub.1-C.sub.3 gases.

A process for producing liquid hydrocarbon products from a biomass-containing feedstock and/or a biomass-derived feedstock is provided. The process comprises: a) contacting the feedstock with a hydropyrolysis catalyst composition and molecular hydrogen in a hydropyrolysis reactor vessel to produce a product stream comprising a partially deoxygenated hydrocarbon product, H.sub.2O, H.sub.2, CO.sub.2, CO, C.sub.1-C.sub.3 gases, char and catalyst fines; b) removing char and catalyst fines from said product stream; c) cooling the remaining product stream to a temperature in the range of from 150 to 400? C.; and d) hydroconverting said partially deoxygenated hydrocarbon product in a hydroconversion reactor in the presence of one or more catalyst compositions suitable for hydrodeoxygenation and aromatic saturation of the partially deoxygenated hydrocarbon product in the presence of H.sub.2O, CO.sub.2, CO, H.sub.2, and C.sub.1-C.sub.3 gas generated in step a), to produce a vapour phase product comprising a C.sub.4+ hydrocarbon product.

Embodiments of the invention include apparatus and systems for hydrocarbon synthesis and methods regarding the same. In an embodiment, the invention includes a method for creating a hydrocarbon product stream comprising reacting a reaction mixture in the presence of a catalyst inside of a reaction vessel to form a product mixture, the reaction mixture comprising a carbon source and water. The temperature inside the reaction vessel can be between 450 degrees Celsius and 600 degrees Celsius and the pressure inside the reaction vessel can be above supercritical pressure for water. In an embodiment, the invention includes an extrusion reactor system for creating a hydrocarbon product stream. The temperature inside the extrusion reactor housing between 450 degrees Celsius and 600 degrees Celsius. Pressure inside the reaction vessel can be above supercritical pressure for water. Other embodiments are also included herein.

The present disclosure relates to a process for the production of crude bio-oil which involves heating a mixture of biomass slurry and a mixed catalyst system in the presence of a hydrogen source at a temperature ranging from 200 to 350 C. and at a pressure ranging from 70 to 250 bars to obtain a mass containing crude bio-oil. The crude bio-oil can then be separated from said mass containing crude bio-oil. The mixed catalyst system remains in solid form and can be easily separated and reused in the next cycle of hydrothermal conversion of biomass to crude bio-oil.

The present disclosure provides a catalyst composition for conversion of biomass to crude bio oil. The composition comprises at least one metal compound, at least one support and at least one stabilizing/solubilizing agent. Also disclosed are processes for the preparation of catalyst composition, and hydrothermal conversion of biomass to crude bio oil.

A bifunctional catalyst for conversion of oxygenates, said catalyst comprising zeolite, alumina binder and Zn, wherein the Zn is present at least partly as ZnAl.sub.2O.sub.4.

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.