A hydrocarbon production method for producing hydrocarbons from a hydrocarbon mixture includes: a first extractive distillation step of performing extractive distillation of an extractive distillation target to obtain a fraction (A) in which isoprene and piperylene are enriched and a fraction (B) in which a linear hydrocarbon and a branched hydrocarbon are enriched; a first distillation step of obtaining a fraction (C) in which isoprene is enriched and a fraction (D) in which piperylene is enriched from the fraction (A); a dehydrogenation step of performing dehydrogenation or oxidative dehydrogenation of either or both of the linear hydrocarbon and the branched hydrocarbon contained in the fraction (B) to obtain a dehydrogenated product; and a recovery step of supplying the dehydrogenated product to an extractive distillation column or a distillation column and obtaining isoprene and/or piperylene from the dehydrogenated product.

A cannabis processing system comprises a grinding apparatus and a cell disruption apparatus. The grinding apparatus is configured to grind wet cannabis cuttings to from a ground, wet cannabis material comprising wet cannabis particles having an average particle size within a range of from about 1 mm to about 3 mm. The cell disruption apparatus is downstream of the grinding apparatus and is configured to disrupt cell walls of plant cells of the wet cannabis particles through one or more of flash freezing, a cellulose solvent, applied negative pressure, and vacuum distillation to facilitate removal of one or more cannabinoids within the plant cells of the wet cannabis particles. Methods of processing cannabis are also described.

The invention relates to a process configuration for production of light olefins and aromatics from residual hydrocarbon streams. In this configuration a high severity catalytic cracking process is employed for producing higher yields of lighter olefins and various boiling fractions. C4 stream separated from gaseous product is subjected to metathesis and aromatized to form mono aromatics.

The invention relates to a process configuration for production of light olefins and aromatics from residual hydrocarbon streams. In this configuration a high severity catalytic cracking process is employed for producing higher yields of lighter olefins and various boiling fractions. C4 stream separated from gaseous product is subjected to metathesis and aromatized to form mono aromatics.

In some examples, a vapor phase product and a liquid phase product can be separated from a heated mixture that can include steam and a hydrocarbon. The liquid phase product can be catalytically cracked in the presence of a fluidized catalyst to produce a catalytically cracked effluent. A bottoms product can be separated from the catalytically cracked effluent. The bottoms product can be hydroprocessed to produce a hydroprocessed product. For example, the bottoms product can be hydroprocessed under pre-treater hydroprocessing conditions to produce a pre-treated bottoms product and the pre-treated bottoms product can be hydroprocessed under bottoms product hydroprocessing conditions to produce the hydroprocessed product. A hydroprocessor heavy product can be separated from the hydroprocessed product. The vapor phase product can be steam cracked to produce a steam cracker effluent. A tar product and an upgraded steam cracker effluent can be separated from the steam cracker effluent.

In some examples, a vapor phase product and a liquid phase product can be separated from a heated mixture that can include steam and a hydrocarbon. The liquid phase product can be catalytically cracked in the presence of a fluidized catalyst to produce a catalytically cracked effluent. A bottoms product can be separated from the catalytically cracked effluent. The bottoms product can be hydroprocessed to produce a hydroprocessed product. For example, the bottoms product can be hydroprocessed under pre-treater hydroprocessing conditions to produce a pre-treated bottoms product and the pre-treated bottoms product can be hydroprocessed under bottoms product hydroprocessing conditions to produce the hydroprocessed product. A hydroprocessor heavy product can be separated from the hydroprocessed product. The vapor phase product can be steam cracked to produce a steam cracker effluent. A tar product and an upgraded steam cracker effluent can be separated from the steam cracker effluent.

This invention relates to production of low sulfur MARPOL compliant bunker fuel oil and distillates using high sulfur residue, low sulfur residue and/or blend of high and low sulfur residue feed stock. The invention also describes a method for production of a cutterstock stream having a lower paraffin and higher aromatic content than a feed stream using a paraffin separation section and its blending to produce bunker fuel.

This invention relates to production of low sulfur MARPOL compliant bunker fuel oil and distillates using high sulfur residue, low sulfur residue and/or blend of high and low sulfur residue feed stock. The invention also describes a method for production of a cutterstock stream having a lower paraffin and higher aromatic content than a feed stream using a paraffin separation section and its blending to produce bunker fuel.

The invention provides a process for separating saturated and unsaturated carboxylic acids is described. The process includes providing a stream comprising same carbon number saturated and unsaturated carboxylic acids; contacting said stream with an extractive solvent in an extractive distillation unit, to produce a first stream comprising extractive solvent and unsaturated carboxylic acids and a second stream comprising saturated carboxylic acids, and feeding said first stream to a solvent recovery unit, to produce a third stream comprising unsaturated carboxylic acids and a fourth stream comprising extractive solvent. In some embodiments, the extractive solvent has a boiling point at atmospheric pressure that is at least 5° C. higher than the boiling point of the unsaturated carboxylic acid.

The invention provides a process for separating saturated and unsaturated carboxylic acids is described. The process includes providing a stream comprising same carbon number saturated and unsaturated carboxylic acids; contacting said stream with an extractive solvent in an extractive distillation unit, to produce a first stream comprising extractive solvent and unsaturated carboxylic acids and a second stream comprising saturated carboxylic acids, and feeding said first stream to a solvent recovery unit, to produce a third stream comprising unsaturated carboxylic acids and a fourth stream comprising extractive solvent. In some embodiments, the extractive solvent has a boiling point at atmospheric pressure that is at least 5° C. higher than the boiling point of the unsaturated carboxylic acid.