A gas stream comprising LPG and naphtha hydrocarbons is absorbed with a sponge absorbent to recover LPG and naphtha hydrocarbons. The gas stream may comprise stripper off gas and/or PSA tail gas. An absorbent stream may be a stripped stream. The stripper off gas stream and the stripped stream may be obtained from a stripper that is downstream of a hydroprocessing unit.

In an FCC apparatus and process structured packing should be located at the very top of the stripping section in an upper region. The lower region below the structural packing may be equipped with fluidization equipment such as stripping media distributors and one or more gratings. This arrangement enables stripping of entrained hydrocarbons off the incoming catalyst immediately upon entry into the stripping section allowing the entrained hydrocarbon to exit the stripping section with minimized residence time to minimize post-riser cracking. Revamp of stripping sections with tall stripping sections should conducted in this way to improve performance and reduce down-time for equipment installation.

A method for thermal processing and catalytic cracking of a biomass to effect distillate oil recovery can include, particle size reduction. slurrying the biomass with a carrier fluid to create a reaction mixture, slurrying a catalyst with a carrier fluid to create a catalyst slurry, heating the reaction mixture and/or the catalyst slurry, and depolymerizing the reaction mixture with the catalyst. The reaction mixture can undergo distillation and fractionation to produce distillate fractions that include naphtha, kerosene, and diesel. In some embodiments, thermal processing and catalytic cracking includes vaporization of the biomass followed by distillation and fractionation. In some embodiments, a resulting distillate can be used as a carrier fluid. In some embodiments, the method can include desulfurization, dehydration, and/or decontamination.

A membrane unit is able to recover hydrogen from a resid waste gas stream. Two membrane units provide even greater hydrogen recovery. The membrane separation is performed at conditions that allow the pressure of the recovered hydrogen to enter into a second stage of compression, saving the expense of the first stage of compression.

This method includes introducing a downstream stream (140) of cracked gas from a downstream heat exchanger (58) in a downstream separator (60) and recovering, at the head of the downstream separator (60), a high-pressure fuel gas stream (144). The method includes the passage of the stream (144) of fuel through the downstream exchanger (58) and an intermediate exchanger (50, 54) to form a reheated high-pressure fuel stream (146), the expansion of the reheated high-pressure fuel stream (146) in at least a first dynamic expander (68) and the passage of the partially expanded fuel stream (148) from the intermediate exchanger (50, 54) in a second dynamic expander (70) to form an expanded fuel stream (152). The expanded fuel stream (152) from the second dynamic expander (70) is reheated in the downstream heat exchanger (58) and in the intermediate heat exchanger (50, 54).

A process for hydrocracking a hydrocarbon feed is provided. The process comprises hydrocracking the hydrocarbon feed to produce a first hydrocracking product stream, separating the first hydrocracking product stream to form a gas stream and a liquid stream, hydrocracking the liquid stream to produce a second hydrocracking product stream, separating the second hydrocracking product stream to form a first light stream and a first heavy stream comprising benzene, toluene, xylene, C.sub.9+ hydrocarbon, or a combination comprising at least one of the foregoing, purifying the gas stream to form a purified gas stream, and separating the purified gas stream to form at least two of a hydrogen stream, C.sub.1 stream, C.sub.2 stream, C.sub.3 stream, C.sub.4 stream, C.sub.5+ stream, or a combination comprising at least one of the foregoing.

A process and system for recovering natural gas liquids (NGL) using a combination of J-T cooling and membrane separation. The process involves compressing, separating, and cooling a flare gas stream comprising at least methane and C.sub.3+ hydrocarbons prior to being introduced to a J-T valve. The cooled stream exiting the J-T valve is further separated, producing a NGL product stream and an uncondensed gas stream. The uncondensed gas stream is directed to a membrane separation step, which results in a C.sub.3+ hydrocarbon enriched stream and a C.sub.3+ hydrocarbon depleted stream. The C.sub.3+ hydrocarbon enriched stream may be recycled back to the process to recover more NGL.

Systems and methods of optimizing enhanced oil recovery fluids in the form of a hydrocarbon foam, an emulsion based foam, an emulsion, and a gelled enhanced oil recovery fluid, each comprising Y-Grade NGL, which is an unfractionated hydrocarbon mixture that comprises ethane, propane, butane, isobutane, and pentane plus, wherein the unfractionated hydrocarbon mixture is a byproduct of a condensed and demethanized hydrocarbon stream.

A method for thermal processing and catalytic cracking of a biomass to effect distillate oil recovery can include, particle size reduction. slurrying the biomass with a carrier fluid to create a reaction mixture, slurrying a catalyst with a carrier fluid to create a catalyst slurry, heating the reaction mixture and/or the catalyst slurry, and depolymerizing the reaction mixture with the catalyst. The reaction mixture can undergo distillation and fractionation to produce distillate fractions that include naphtha, kerosene, and diesel. In some embodiments, thermal processing and catalytic cracking includes vaporization of the biomass followed by distillation and fractionation. In some embodiments, a resulting distillate can be used as a carrier fluid. In some embodiments, the method can include desulfurization, dehydration, and/or decontamination.

This method comprises passing a residual stream into a flash drum to form a gaseous overhead flow and liquid bottom flow, and feeding the bottom flow into a distillation column,

It comprises cooling the overhead flow in a heat exchanger to form a cooled overhead flow.

It comprises the extraction of a gaseous overhead stream at the head of the distillation column, and the formation of at least one effluent stream from the overhead stream and/or from the top stream.

The separation of the cooled overhead flow flow comprises passing the cooled overhead flow into an absorber, and injecting a methane-rich stream into the absorber to place the cooled overhead flow in contact with the methane-rich stream.