A multi-stage process for reducing the environmental contaminants in an ISO8217 compliant Feedstock Heavy Marine Fuel Oil involving a core desulfurizing process and a ultrasound treatment process as either a pre-treating step or post-treating step to the core process. The Product Heavy Marine Fuel Oil complies with ISO 8217 for residual marine fuel oils and has a sulfur level has a maximum sulfur content (ISO 14596 or ISO 8754) between the range of 0.05 mass % to 1.0 mass. A process plant for conducting the process is also disclosed.

The invention relates to systems and methods for ultrasonic oxidative desulfurization of heavy fuel oils. In various embodiments, the methods include combinations of ultrasonic sulfone decomposition processes and/or catalytic decomposition processes.

Provided is a method for producing organic molecules having at least two carbon atoms chained together by the reaction of a hydrogen-containing source, a carbon-containing source and an optional nitrogen-containing source in the presence of a nanostructure or nanostructures, wherein the reaction is initiated by heat.

The present invention relates to a process for hydroconversion of a heavy hydrocarbon feedstock in the presence of hydrogen, at least one supported solid catalyst and at least one dispersed solid catalyst obtained from at least one salt of a heteropolyanion combining molybdenum and at least one metal selected from cobalt and nickel in a Strandberg, Keggin, lacunary Keggin or substituted lacunary Keggin structure.

A catalytic process for the deoxygenation of an organic substrate, such as a biomass or bio-oil, is described. The catalytic process is conducted in the presence of a gaseous mixture containing both hydrogen and nitrogen. The presence of nitrogen in the gaseous mixture gives rise inter-aliato increased catalytic activity and/or increased selectivity for aromatic reaction products.

An ebullated bed hydroprocessing system is upgraded and operated at modified conditions using a dual catalyst system to produce less fouling sediment. The less fouling sediment produced by the upgraded ebullated bed reactor reduces the rate of equipment fouling at any given sediment production rate and/or concentration compared to the sediment produced by the ebullated bed reactor prior to upgrading. In some cases, sediment production rate and/or concentration are maintained or increased, after upgrading the ebullated bed reactor, while equipment fouling is reduced. In other cases, sediment production rate and/or concentration are increased, after upgrading the ebullated bed reactor, without increasing equipment fouling. In some cases, sediment production rate and/or concentration are decreased by a given percentage, after upgrading the ebullated bed reactor, and the rate of equipment fouling is decreased by a substantially greater percentage.

Provided is a process for preparing base oil from a waxy hydrocarbon feedstock by contacting the hydrocarbon feedstock in a hydroisomerization zone under hydroisomerization conditions. The reaction is in the presence of hydrogen and an inert gas, with the total pressure in the hydroisomerization zone being at least 400 psig. A product from the hydroisomerization zone is collected and separated into base oil products and fuel products. The inert gas can comprise any suitable inert gas, but is generally nitrogen, methane or argon. Nitrogen is used in one embodiment.

Processes and systems for producing raw materials and for producing truly circular polymers. The systems and processes may include processing a waste-derived hydrocarbon stream, such as a waste plastic pyrolysis oil, in a first reactor system with a catalyst mixture, and processing a fossil-based feedstock in a second reactor system with the catalyst mixture. The catalyst mixture may be supplied to each of the first and second reactor systems from a common catalyst regenerator. An effluent comprising fossil-based hydrocarbon products may be recovered from the second reactor system, and an effluent comprising waste-derived hydrocarbon products may be recovered from the first reactor system. Following separations, spent catalyst from each of the first and second reactor systems may be returned to the common catalyst regenerator.

The catalytic cracking catalyst contains a molecular sieve and an alumina substrate material. The alumina substrate material has a crystalline phase structure of γ-alumina. Based on the volume of pores with a diameter of 2-100 nm, the pore volume of the pores with a diameter of 2-5 nm accounts for 0-10%, the pore volume of the pores with a diameter of more than 5 nm and not more than 10 nm accounts for 10-25%, and the pore volume of the pores with a diameter of more than 10 nm and not more than 100 nm accounts for 65-90%.

Systems are provided that permit temperature control of a catalyst bed for conversion of alcohols to fuel hydrocarbons by modulating the water content of the alcohol feed stream provided to the catalyst bed. In some embodiments a secondary catalyst bed is provided for the conversion of light hydrocarbons found in the initial hydrocarbon product to fuel hydrocarbons that are liquid at ambient temperature and pressure.