A catalyst is provided for hydrodeoxygenation and hydroisomerization of paraffins having higher activity. The catalyst contains a molecular sieve, such as SAPO-11, a metal component such as platinum and/or palladium or nickel tungsten sulfide or nickel molybdenum sulfide and a binder such as gamma alumina. The catalyst exhibits a high proportion of weak acid sites and a relatively equal distribution of the metal component on the molecular sieve and the binder.

The present disclosure provides methods for fabricating catalysts for ammonia decomposition. The method may comprise (a) subjecting a catalyst support to one or more physical or chemical processes to optimize one or more pores, morphologies, and/or surface chemistry or property of the catalyst support; (b) depositing a composite support material on the catalyst support, wherein the composite support material comprises a morphology or surface chemistry or property; and (c) depositing one or more active metals on at least one of the composite support material and the catalyst support, wherein the one or more active metals comprise one or more nanoparticles configured to conform to the morphology of the composite support material and/or catalyst support material, thereby optimizing one or more active sites on the nanoparticles for ammonia processing.

The present disclosure provides methods for fabricating catalysts for ammonia decomposition. The method may comprise (a) subjecting a catalyst support to one or more physical or chemical processes to optimize one or more pores, morphologies, and/or surface chemistry or property of the catalyst support; (b) depositing a composite support material on the catalyst support, wherein the composite support material comprises a morphology or surface chemistry or property; and (c) depositing one or more active metals on at least one of the composite support material and the catalyst support, wherein the one or more active metals comprise one or more nanoparticles configured to conform to the morphology of the composite support material and/or catalyst support material, thereby optimizing one or more active sites on the nanoparticles for ammonia processing.

Methods of heating a reactor system by providing electrical energy are described. A reactor system comprising at least one reactor tube having a catalyst disposed therein and comprises at least one electrically conductive surface is heated by providing electrical energy to the at least one electrically conductive surface on the reactor tube and adjusting a current level of the electrical energy provided to the at least one electrically conductive surface to control the temperature of the reactor tube and the catalyst disposed therein. The reactor tube may be electrically isolated from other electrically conductive components of the reactor system.

Methods of heating a reactor system by providing electrical energy are described. A reactor system comprising at least one reactor tube having a catalyst disposed therein and comprises at least one electrically conductive surface is heated by providing electrical energy to the at least one electrically conductive surface on the reactor tube and adjusting a current level of the electrical energy provided to the at least one electrically conductive surface to control the temperature of the reactor tube and the catalyst disposed therein. The reactor tube may be electrically isolated from other electrically conductive components of the reactor system.

Disclosed are shaped dehydrogenation catalysts, methods for making the catalysts, and methods for dehydrogenating a hydrocarbon using the catalyst. A method for making the shaped dehydrogenation catalyst can include combining a group 13 metal precursor and a group 1 metal precursor with a catalyst support precursor to form a shapeable material, shaping the shapeable material to form a wet shaped material, drying the wet shaped material to form a dry shaped material, and calcining the dry shaped material to form the shaped dehydrogenation catalyst.

Disclosed are shaped dehydrogenation catalysts, methods for making the catalysts, and methods for dehydrogenating a hydrocarbon using the catalyst. A method for making the shaped dehydrogenation catalyst can include combining a group 13 metal precursor and a group 1 metal precursor with a catalyst support precursor to form a shapeable material, shaping the shapeable material to form a wet shaped material, drying the wet shaped material to form a dry shaped material, and calcining the dry shaped material to form the shaped dehydrogenation catalyst.

A catalyst has a carrier and a hydrogenation active metal component supported on the carrier. The hydrogenation active metal component contains at least one Group VIB metal component and at least one Group VIII metal component, and the carrier is composed of phosphorus-containing alumina. When the hydrogenation catalyst is measured using a hydrogen temperature programmed reduction method (H.sub.2-TPR), the ratio of the peak height of the low-temperature reduction peak, P.sub.low-temp peak, at a temperature of 300-500° C. to the peak height of the high-temperature reduction peak, P.sub.hi-temp peak, at a temperature of 650-850° C., i.e. S=P.sub.low-temp peak/P.sub.hi-temp peak, is 0.5-2.0; preferably 0.7-1.9, and more preferably 0.8-1.8. The hydrogenation catalyst shows excellent heteroatom removal effect and excellent stability when used in hydrotreatment.

A catalyst has a carrier and a hydrogenation active metal component supported on the carrier. The hydrogenation active metal component contains at least one Group VIB metal component and at least one Group VIII metal component, and the carrier is composed of phosphorus-containing alumina. When the hydrogenation catalyst is measured using a hydrogen temperature programmed reduction method (H.sub.2-TPR), the ratio of the peak height of the low-temperature reduction peak, P.sub.low-temp peak, at a temperature of 300-500° C. to the peak height of the high-temperature reduction peak, P.sub.hi-temp peak, at a temperature of 650-850° C., i.e. S=P.sub.low-temp peak/P.sub.hi-temp peak, is 0.5-2.0; preferably 0.7-1.9, and more preferably 0.8-1.8. The hydrogenation catalyst shows excellent heteroatom removal effect and excellent stability when used in hydrotreatment.

A method for producing a three-dimensional porous transition alumina catalyst monolith of stacked catalyst fibers, comprising: a) Preparing a paste in a liquid diluent of hydroxide precursor particles and/or oxyhydroxide precursor particles of transition alumina particles, all particles in the suspension having a number average particle size in the range of from 0.05 to 700 μm, b) extruding the paste nozzle(s) to form fibers, and depositing the extruded fibers to form a three-dimensional porous catalyst monolith precursor, c) drying the precursor to remove the liquid diluent, d) performing a temperature treatment of the dried porous catalyst monolith precursor to form the transition alumina catalyst monolith, wherein no temperature treatment of the porous catalyst monolith precursor or porous catalyst monolith at temperatures above 1000° C. is performed and wherein no further catalytically active metals, metal oxides or metal compounds are applied to the surface.