A liquid phase alkylation product from an alkylation reaction unit is introduced into a first heat-exchanger directly or after being pressurized with a pressure pump and heat-exchanged with a vapor phase stream from the column top of a high-pressure fractionating column n, then introduced into a second heat-exchanger and further heated to 100° C.-150° C., then introduced into the high-pressure fractionating column and subjected to fractionation at 2.0 MPa-4.0 MPa, the vapor phase stream from the column top of the high-pressure fractionating column is heat-exchanged with the liquid phase alkylation product to be separated, a liquid phase stream from the column bottom of the high-pressure fractionating column is introduced into a low-pressure fractionating column and subjected to fractionation under at 0.2 MPa-1.0 MPa, a low-carbon alkane is obtained from the column top of the low-pressure fractionating column n, and a liquid phase stream obtained from the column bottom of the low-pressure fractionating column is an alkylation oil product.

Processes for alkylating benzene are provided. In embodiments, the process comprises combining benzene, an olefin, and a catalyst composition under conditions to react benzene with the olefin to produce an alkylbenzene, the catalyst composition comprising components selected from the group consisting of an ionic liquid, an acid, and an aromatic; an acid, a base capable of forming an ionic liquid with the acid, and an aromatic; an ionic liquid and an acid; and an acid and a base capable of forming an ionic liquid with the acid. The ionic liquid does not comprise a metal halide and the catalyst composition is free of a metal halide and the aromatic, if present in the catalyst composition, is not the benzene being alkylated.

Processes for alkylating benzene are provided. In embodiments, the process comprises combining benzene, an olefin, and a catalyst composition under conditions to react benzene with the olefin to produce an alkylbenzene, the catalyst composition comprising components selected from the group consisting of an ionic liquid, an acid, and an aromatic; an acid, a base capable of forming an ionic liquid with the acid, and an aromatic; an ionic liquid and an acid; and an acid and a base capable of forming an ionic liquid with the acid. The ionic liquid does not comprise a metal halide and the catalyst composition is free of a metal halide and the aromatic, if present in the catalyst composition, is not the benzene being alkylated.

Methods and systems for steam cracking a mixed butane containing feed stream are disclosed. The feed stream includes n-butane and isobutane. The disclosed methods and systems entail splitting the feed into an enriched n-butane fraction and an enriched isobutane fraction. The enriched n-butane fraction is provided to the cracking furnaces, which yield the olefin products and also yield C4 species. The C4 species are partially hydrogenated and provided as a reactant feed to an alkylation reaction. The enriched isobutane fraction is also provided to the alkylation reaction, whereby high value alkylate product is produced. The disclosed methods and systems have increase olefins (especially ethylene) yield because the feed to the cracking process is enriched in n-butane. The economics are also improved because high value alkylate product is produced from a portion of the isobutane.

Methods and systems for steam cracking a mixed butane containing feed stream are disclosed. The feed stream includes n-butane and isobutane. The disclosed methods and systems entail splitting the feed into an enriched n-butane fraction and an enriched isobutane fraction. The enriched n-butane fraction is provided to the cracking furnaces, which yield the olefin products and also yield C4 species. The C4 species are partially hydrogenated and provided as a reactant feed to an alkylation reaction. The enriched isobutane fraction is also provided to the alkylation reaction, whereby high value alkylate product is produced. The disclosed methods and systems have increase olefins (especially ethylene) yield because the feed to the cracking process is enriched in n-butane. The economics are also improved because high value alkylate product is produced from a portion of the isobutane.

Methods and systems for steam cracking a mixed butane containing feed stream are disclosed. The feed stream includes n-butane and isobutane. The disclosed methods and systems entail splitting the feed into an enriched n-butane fraction and an enriched isobutane fraction. The enriched n-butane fraction is provided to the cracking furnaces, which yield the olefin products and also yield C4 species. The C4 species are partially hydrogenated and provided as a reactant feed to an alkylation reaction. The enriched isobutane fraction is also provided to the alkylation reaction, whereby high value alkylate product is produced. The disclosed methods and systems have increase olefins (especially ethylene) yield because the feed to the cracking process is enriched in n-butane. The economics are also improved because high value alkylate product is produced from a portion of the isobutane.

The present disclosure relates to a method and an apparatus for self-heat-extracting flash evaporation of a sulfuric acid alkylation reaction product. There is provided a method for self-heat-extracting flash evaporation of a sulfuric acid alkylation reaction product. One step is to coalesce and vaporize a preliminarily distributed sulfuric acid alkylation reaction product to cause preliminary vaporization of a hydrocarbon therein, thereby taking heat away and preliminarily separating the hydrocarbon from sulfuric acid. Another step is to subject the preliminarily separated alkylation reaction to reinforced separation, where the hydrocarbon is further vaporized to take heat away and further separate the hydrocarbon from the sulfuric acid. There is also provided an apparatus for self-heat-extracting flash evaporation of a sulfuric acid alkylation reaction product.

The present disclosure relates to a method and an apparatus for self-heat-extracting flash evaporation of a sulfuric acid alkylation reaction product. There is provided a method for self-heat-extracting flash evaporation of a sulfuric acid alkylation reaction product. One step is to coalesce and vaporize a preliminarily distributed sulfuric acid alkylation reaction product to cause preliminary vaporization of a hydrocarbon therein, thereby taking heat away and preliminarily separating the hydrocarbon from sulfuric acid. Another step is to subject the preliminarily separated alkylation reaction to reinforced separation, where the hydrocarbon is further vaporized to take heat away and further separate the hydrocarbon from the sulfuric acid. There is also provided an apparatus for self-heat-extracting flash evaporation of a sulfuric acid alkylation reaction product.

A solid acid catalyst has a macropore specific volume of about 0.30-0.50 ml/g, a ratio of macropore specific volume to specific length of catalyst particles of about 1.0-2.5 ml/(g.Math.mm), and a ratio of specific surface area to length of catalyst particles of about 3.40-4.50 m.sup.2/mm. The macropore refers to pores having a diameter of more than 50 nm. An alkylation catalyst is based on the solid acid catalyst and can be used in alkylation reactions. The solid acid catalyst and alkylation catalyst show an improved catalyst service life and/or trimethylpentane selectivity when used in the alkylation of isoparaffins with olefins.

A solid acid catalyst has a macropore specific volume of about 0.30-0.50 ml/g, a ratio of macropore specific volume to specific length of catalyst particles of about 1.0-2.5 ml/(g.Math.mm), and a ratio of specific surface area to length of catalyst particles of about 3.40-4.50 m.sup.2/mm. The macropore refers to pores having a diameter of more than 50 nm. An alkylation catalyst is based on the solid acid catalyst and can be used in alkylation reactions. The solid acid catalyst and alkylation catalyst show an improved catalyst service life and/or trimethylpentane selectivity when used in the alkylation of isoparaffins with olefins.