Systems and methods for producing butadiene are disclosed. In a reaction unit, n-butane is dehydrogenated in the presence of a double-dehydrogenation catalyst to produce a mixture that includes butadiene and unreacted n-butane. An extractive distillation unit that uses soybean oil as the solvent is utilized to extract at least some of the unreacted n-butane from the mixture.

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.

The present disclosure provides a method of separating α-olefin by a simulated moving bed. The method comprises using a coal-based Fischer-Tropsch synthetic oil as a raw material to obtain a target olefin having a carbon number N within a range from 9 to 18, wherein the raw material is subjected to treatment steps including pretreatment, fraction cutting, alkane-alkene separation, and isomer separation, thereby obtaining a high purity α-olefin product. As compared to conventional rectification and extraction processes, the product obtained by the method of the present disclosure has advantages of higher purity, higher yield, lower energy consumption, and significantly reduced production cost.

A process for producing olefins from the hydrocarbon feed includes introducing the hydrocarbon feed into a Solvent Deasphalting Unit (SDA) to remove asphaltene from the hydrocarbon feed producing a deasphalted oil stream, wherein the SDA comprises a solvent that reacts with the hydrocarbon feed, and the deasphalted oil stream comprises from 0.01 weight percent (wt. %) to 18 wt. % asphaltenes; introducing the deasphalted oil stream into a steam catalytic cracking system; steam catalytically cracking the deasphalted oil stream in the steam catalytic cracking system in the presence of steam and a nano zeolite cracking catalyst to produce a steam catalytic cracking effluent; and separating the olefins from the steam catalytic cracking effluent.

Methods and systems for treating an olefin-containing stream are disclosed. The disclosed methods and systems are particularly suitable for treating an off-gas stream in a refining or petrochemical process, such as from a fluid catalytic cracker (FCC), coker, steam cracker, and the like. The stream is treated in an absorber column to reject lighter stream components and to absorb ethylene and/or propylene into a solvent. The solvent is typically isobutane. The enriched solvent stream from the absorber column is fed to an alkylation reactor, which reacts the dissolved olefin with the isobutane solvent to produce an alkylate product.

A method of producing a fuel additive includes passing a feed stream comprising C.sub.4 hydrocarbons through a first hydrogenation unit producing a first process stream; passing the first process stream through a distillation unit; withdrawing a 2-butene stream from the distillation unit: passing the 2-butene stream through a second hydrogenation unit producing a 1-butene stream; passing at least a portion of the 1-butene stream through a separation unit; and passing the 1-butene stream through a hydration unit producing the fuel additive.

Described is a process for producing field butane. The process includes increasing the n-butane concentration in field butane. The process may include a concentration process that includes distillation and a thermal cracking process.

A process of recovering propylene and N-butyraldehyde from a purge gas includes forming a first product stream including N-butyraldehyde by reacting propylene and a first synthesis gas in the presence of a first catalyst in a first reactor and a second reactor; withdrawing a mixed stream from the second reactor; separating a liquid stream and purge gas from the mixed stream and recycling the liquid stream to the second reactor; reacting the purge gas and a second synthesis gas in the presence of a second catalyst in a purge gas reactor to form a second product stream including N-butyraldehyde; withdrawing the second product stream including N-butyraldehyde from the purge gas reactor and combining the second product stream including N-butyraldehyde and the first product stream including N-butyraldehyde; and withdrawing a stream including N-butyraldehyde from the purge gas reactor and recovering N-butyraldehyde from the stream including N-butyraldehyde product stream.

A method for preparing 2-alkylanthracene includes the step of separating 2-alkylanthracene from a reaction product of anthracene alkylation reaction. The anthracene alkylation reaction is a reaction of anthracene and an alkylation reagent under an alkylation condition and in the presence of an alkylation reaction solvent and a catalyst. The reaction product of the anthracene alkylation reaction contains anthracene and the product of a series of alkylanthracenes containing 2-alkylanthracene.

A method for separating classes of hydrocarbon compounds from a feed stream including a hydrocarbon mixture is disclosed. The method includes the steps of passing a feed stream through a plurality of separation units arranged in a series in any order, wherein each separation unit has an adsorbent material; and separating classes of hydrocarbon compounds from the feed stream. When one of the plurality of separation units comprises an adsorbent material that is a metal organic framework selected from a zirconium, hafnium, cerium, or titanium-based metal organic framework, then another plurality of separation units includes an adsorption material that is different from the metal organic framework. The method is conducted in a liquid phase. The method can also use a single separation unit with a continuous cyclic bed apparatus. The method can be combined with refining and downstream processes.