A liquid-solid axial moving bed reaction and regeneration apparatus and a solid acid alkylation process by using the liquid-solid axial moving bed reaction and regeneration apparatus. the liquid-solid axial moving bed reaction and regeneration apparatus comprise:

An axial moving bed reactor (1), a spent catalyst receiver (5), a catalyst regenerator (4) and a regenerated catalyst receiver (6) that are successively connected, wherein, a catalyst outlet of the regenerated catalyst receiver (6) is communicated with a catalyst inlet of the axial moving bed reactor (1);

Wherein, the axial moving bed reactor (1) is provided with at least two catalyst beds (3) arranged up and down, the axial moving bed reactor (1) is provided with a feed inlet (2) above each catalyst bed (3);

A catalyst delivery pipe (16) is arranged between two adjacent catalyst beds (3) so that the catalyst can move from top to bottom in the axial moving bed reactor (1);

A separation component (10) is provided between two adjacent catalyst beds (3), the inside space of the separation component (10) is communicated with the catalyst delivery pipe (16), the separation component (10) is for separating the stream after the reaction in the upstream catalyst bed from the catalyst, the catalyst obtained by the separation with the separation component (10) moves down through the catalyst delivery pipe (16).

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.

Processes for the direct alkylation of ethylene with isobutane or isopentane using a highly active ionic liquid alkylation catalyst are described. Ethylene is sent to a high-temperature alkylation reactor loop, and C.sub.3, C.sub.4, and C.sub.5 olefins are routed to a low temperature alkylation reactor loop. In each reactor, the olefins are contacted with an excess of isobutane or isopentane in the presence of a highly active ionic liquid catalyst. Portions of the reactor effluent streams are fed to a common downstream catalyst separation and product fractionation sections. The remainder of the reactor effluent is recycled back to the respective alkylation reactor.

Processes for the direct alkylation of ethylene with isobutane or isopentane using a highly active ionic liquid alkylation catalyst are described. Ethylene is sent to a high-temperature alkylation reactor loop, and C.sub.3, C.sub.4, and C.sub.5 olefins are routed to a low temperature alkylation reactor loop. In each reactor, the olefins are contacted with an excess of isobutane or isopentane in the presence of a highly active ionic liquid catalyst. Portions of the reactor effluent streams are fed to a common downstream catalyst separation and product fractionation sections. The remainder of the reactor effluent is recycled back to the respective alkylation reactor.

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 n≥1 and n≥m. 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.

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 n≥1 and n≥m. 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.

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 n≥1 and n≥m. 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.

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.