Power recovery turbines can be used debottlenecking of an existing plant, as well as recover electric power when revamping a plant. A process for recovering energy in a petroleum, petrochemical, or chemical plant is described. A fluid stream having a first control valve thereon is identified. A first power-recovery turbine is installed at the location of the first control valve, and at least a portion of the first fluid stream is directed through the first power-recovery turbine to generate electric power as direct current therefrom. The electric power is then recovered.

The present disclosure relates to the thermal liquefaction of lignin, and more particularly to lignin solvolysis of a lignin feedstock chosen based on its molecular weight. The process comprises subjecting a feed mixture (30) of lignin feedstock (10) and solvent (20) to a thermal liquefaction step by heating (110) the feed mixture (30) at a temperature between 360 and 420? C., separating (120) a liquid product mix (50) from a product mix (40); and recirculating at least part of said liquid product mix (50) as an oil fraction of said solvent (20).

The present disclosure relates to the thermal liquefaction of lignin, and more particularly to lignin solvolysis of a lignin feedstock chosen based on its molecular weight. The process comprises subjecting a feed mixture (30) of lignin feedstock (10) and solvent (20) to a thermal liquefaction step by heating (110) the feed mixture (30) at a temperature between 360 and 420? C., separating (120) a liquid product mix (50) from a product mix (40); and recirculating at least part of said liquid product mix (50) as an oil fraction of said solvent (20).

A computer-implemented method and system for modeling chemical reaction in a chemical reactor is disclosed. The method and system employ a molecule-based equation-oriented approach. Local-stored pre-estimated thermodynamic properties are generated based on a set of homologous series of compounds defined by the method and system. A set of reaction rate equations is automatically generated in equation-oriented format based on the defined set of homologous series of compounds, a system-defined set of permissible reactions, system-defined properties of the reactor compounds, and the locally-stored pre-estimated thermodynamic properties. The automatically generated set of reaction rate equations forms the model of chemical reactions in the chemical reactor.

An apparatus includes at least one processor configured to obtain inline measurements of one or more properties of crude oil, translate the measurements into a set of process and control parameters, and apply the process and control parameters to process equipment. The process and control parameters configure the process equipment to process the crude oil having the one or more properties. The one or more properties of the crude oil may include at least one of: density, specific gravity, viscosity, carbon residue, and sulfur content of the crude oil. The process and control parameters could be applied to one or more controllers associated with a blending unit in a refinery or to one or more controllers associated with a crude oil distillation column in the refinery.

A catalyst composition comprising a support comprising a mixture of amorphous silica-alumina and non-zeolitic alumina comprising no more than 75 wt % amorphous silica-alumina and having a ratio of moles of silicon to moles of aluminum in the range of about 0.05 to about 0.50. A first hydrogenation metal comprising platinum, a second hydrogenation metal from Group VIIB or Group VIII of the Periodic Table other than platinum and an optional third metal from Group IA of the Periodic Table may be deposited on the support. The ratio of moles of silicon to the moles of the first hydrogenation metal, the second hydrogenation metal and the optional third metal on the support may be between about 15 and about 75.

A catalyst composition comprising a support comprising a mixture of amorphous silica-alumina and non-zeolitic alumina comprising no more than 75 wt % amorphous silica-alumina and having a ratio of moles of silicon to moles of aluminum in the range of about 0.05 to about 0.50. A first hydrogenation metal comprising platinum, a second hydrogenation metal from Group VIIB or Group VIII of the Periodic Table other than platinum and an optional third metal from Group IA of the Periodic Table may be deposited on the support. The ratio of moles of silicon to the moles of the first hydrogenation metal, the second hydrogenation metal and the optional third metal on the support may be between about 15 and about 75.

A method of controlling the supply and allocation of hydrogen gas in a hydrogen system of a refinery integrated with olefins and aromatics plants to convert crude oil into petrochemicals. The method includes one or more supply sources that provide hydrogen at individual rates, purities, pressures and costs, multiple consumption sites that consume hydrogen at individual rates, purities and pressures and an interconnecting hydrogen distribution network. The method further includes the integration of hydrogen consuming process units with hydrogen producing process units in which hydrogen recovered from the effluents from the hydrogen consuming process units and hydrogen recovered from the hydrogen producing process units are re-used in the hydrogen consuming process units.

A method of controlling the supply and allocation of hydrogen gas in a hydrogen system of a refinery integrated with olefins and aromatics plants to convert crude oil into petrochemicals. The method includes one or more supply sources that provide hydrogen at individual rates, purities, pressures and costs, multiple consumption sites that consume hydrogen at individual rates, purities and pressures and an interconnecting hydrogen distribution network. The method further includes the integration of hydrogen consuming process units with hydrogen producing process units in which hydrogen recovered from the effluents from the hydrogen consuming process units and hydrogen recovered from the hydrogen producing process units are re-used in the hydrogen consuming process units.

An ebullated bed hydroprocessing system is upgraded using a dual catalyst system that includes a heterogeneous catalyst and dispersed metal sulfide particles to produce less fouling sediment. The dual catalyst system more effectively converts sediment-forming precursors to produce sediment that is less fouling than sediment produced using only the heterogeneous catalyst and not the dispersed metal sulfide particles. The dual catalyst system provides for a lower rate of equipment fouling for a given sediment production rate and/or concentration. In some cases, sediment production rate and/or concentration can be maintained or increased while equipment fouling is reduced. In some cases, sediment production rate and/or concentration can be increased without increasing equipment fouling.