A process for acid catalyzed alkylation involving the use of surfactants which form bi-continuous micro-emulsions with the liquid acid and the hydrocarbon is described. The bicontinuous phase formed between the hydrocarbon and liquid acid phases at surfactant addition facilitates and improves the liquid acid catalyzed alkylation reactions including motor-fuel alkylation reaction.

This disclosure relates to alkylation processes. The process involves providing two or more reaction zones disposed in sequence. In at least the first two reaction zones, olefin mixture comprising C3 and C4 olefins is contacted with isoparaffin comprising isobutane in the presence of sulfuric acid solution under effective alkylation conditions to produce a product mixture comprising spent acid solution and alkylate product, wherein the molar ratio of C3 to C4 olefins in the olefin mixture decreases in each subsequent reaction zone. In the process, the sulfuric acid solution present in a reaction zone contains the spent acid solution produced in the immediately preceding reaction zone.

An amorphous molecular material having stilbene and benzyl group substituents at both side of stilbene has fluorescent characteristics.

This disclosure relates to methods of converting an HF alkylation unit which utilizes HF as a reaction catalyst to a sulfuric acid alkylation unit which utilizes sulfuric acid as a reaction catalyst. This disclosure also relates to a segmented sulfuric acid settler for separating a sulfuric acid phase from a hydrocarbon phase. This disclosure also relates to methods of converting a vertical HF acid settler to a segmented sulfuric acid settler. This disclosure also relates to converted sulfuric acid alkylation units and alkylation processes performed in the converted sulfuric acid alkylation units.

Disclosed are a system device for preparing an alkylate oil using a sulfuric acid catalyst and a manufacturing method thereof. The system device comprises a reactor unit (100), a catalyst and hydrocarbon circulation unit (200), a separator unit (300), an isobutane circulation unit (500) and a fractionator unit (400). The reactor unit (100) is connected and in communication with the catalyst and hydrocarbon circulation unit (200) and the separator unit (300) via channels respectively. The catalyst and hydrocarbon circulation unit (200) is connected and in communication with the separator unit (300) via channels. The separator unit (300) is connected and in communication with the isobutane circulation unit (500) and the fractionator unit (400) via channels respectively. The catalyst and hydrocarbon circulation unit (200), the separator unit (300), the isobutane circulation unit (500) and the fractionator unit (400) are connected and in communication with the reactor unit (100) via channels respectively. The reactor unit (100) comprises at least a high gravity reactor. Due to the adopted high gravity reactor capable of highly reinforcing the mixing of materials under high viscosity, the system device can operate at a low temperature of 5 C. and prepare the alkylate oil having an octane number of 97-100 at an alkane/alkene ratio of 2-100.

A method for purifying 1-hexene is disclosed. The method can include contacting a first stream containing 1-hexene and 2-ethyl-1-butene with an isomerization catalyst containing an comprising an alumina, silica-alumina, a zeolite, or an ion exchange resin, or any combinations thereof, under conditions sufficient to selectively isomerize at least a portion of 2-ethyl-1-butene into 3-methyl-2-pentene and form a second stream containing 1-hexene and 3-methyl-2-pentene, and separating the second stream into a third stream containing 1-hexene and a fourth stream containing 3-methyl-2-pentene.

An alkylation reaction apparatus has n reactors. In the n reactors, there are m reactors including the first reactor that have three reaction zones as defined below. According to the flow direction order of alkylation reaction streams, the three reaction zones are an x reaction zone, a y reaction zone and a z reaction zone respectively; based on the mixing intensity, the mixing intensity of the y reaction zone>the mixing intensity of the x reaction zone>the mixing intensity of the z reaction zone, wherein n1 and nm. An alkylation reaction system includes the aforementioned alkylation reaction apparatus, and a liquid acid catalyzed alkylation reaction process by using the aforementioned alkylation reaction apparatus or the aforementioned alkylation reaction system.

The present invention relates to a process for preparing alkyl methacrylates, especially MMA, and methacrylic acid, based on methacrolein, which has been oxidatively esterified in a second process stage. Methacrolein is obtainable in principle from C.sub.2 and C.sub.4 units. The present process has the advantage that the alkyl methacrylate and methacrylic acid can be obtained in a simple manner, in high yields and high purities, either as a mixture or as isolated product streams. In particular, the process of the invention has the great advantage that especially the ratio of the desired methacrylic acid and alkyl methacrylate, especially MMA, products can be adjusted freely within a wide range and varied by chemical engineering measures and operating parameters.

A spent sulfuric acid catalyst from an alkylation unit is regenerated via a paired oxidation electrolysis, wherein active intermediates are generated via both anodic oxidation and cathodic reduction without adding an additional organic peroxide during the electrolysis. The organic impurities in the spent sulfuric acid catalyst are decomposed by the active intermediates, and removed therefrom via evaporation.

The present invention relates to the integration of an alkylation unit for use in a hydrocarbon conversion process. More specifically, the present invention relates to the integration of a dehydrogenation unit and an alkylation unit and the placement of different isomerization units located off the deisobutanizer and the debutanizer.