Abstract: 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.

Abstract: 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.

Abstract: An apparatus for preparing polyalpha-olefins includes a mixing unit, a microchannel reaction unit, a high-pressure separation unit, a low-pressure separation unit, a gas circulation unit, a post-treatment unit and a pressure control unit, the mixing unit, the microchannel reaction unit, the high-pressure separation unit, the low-pressure separation unit that are successively connected. The gas circulation unit, the microchannel reaction unit is provided with the BF3 gas inlet, the mixing unit is provided with the auxiliary feed inlet, and the olefin raw material inlet, the gas circulation unit is connected with the BF3 gas inlet, the low-pressure separation unit is further connected with the post-treatment unit, and the high-pressure separation unit, the pressure control unit, and the gas circulation unit are further successively connected.

Abstract: An apparatus for preparing polyalpha-olefins has an input unit (1), a microchannel reactor (2), and a post-treatment unit (3) that are successively connected. The input unit has a mixer and/or pipeline(s) for delivering an olefin raw material, an auxiliary feed and a BF3 catalyst to the microchannel reactor (2). The apparatus and process that utilizes the apparatus allow flexible and rapid mixing of the catalyst, the auxiliary feed and the olefin raw material, and have the advantages of high polymerization reaction speed, good mass and heat transfer effects, high reaction conversion, good product selectivity and excellent performance, thereby being suitable for large-scale industrial production.

Abstract: A process for separating an alkylation product includes introducing a liquid phase alkylation product from an alkylation reaction unit 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, then into a second heat-exchanger and subsequently into the high-pressure fractionating column. 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 a condition of 0.2 MPa-1.0 MPa, a low-carbon alkane is obtained from the column top of the low-pressure fractionating column, and a liquid phase stream obtained from the column bottom of the low-pressure fractionating column is an alkylation oil product.

Abstract: 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.

Abstract: 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.

Abstract: A liquid-solid radial moving bed reaction apparatus and a solid acid alkylation process by using the liquid-solid radial moving bed reaction apparatus, the liquid-solid radial moving bed reaction apparatus comprises: A radial moving bed reactor, a spent catalyst receiver, a catalyst regenerator, and a regenerated catalyst receiver that are successively connected, wherein the catalyst discharging outlet of the regenerated catalyst receiver is communicated with the catalyst inlet of the radial moving bed reactor; a reaction stream distribution zone, a catalyst bed, and a stream-after-the-reaction collection zone are arranged in the radial moving bed reactor from the inside to the outside or from the outside to the inside, the reaction stream distribution zone is communicated with the reaction stream feeding pipeline; the stream-after-the-reaction collection zone is communicated with the stream-after-the-reaction withdrawing pipe; A component-based mixer is arranged on the reaction stream feeding pipeline; the c

Abstract: 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.

Abstract: A process for separating an alkylation product includes introducing a liquid phase alkylation product from an alkylation reaction unit 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, then into a second heat-exchanger and subsequently into the high-pressure fractionating column. 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 a condition of 0.2 MPa-1.0 MPa, a low-carbon alkane is obtained from the column top of the low-pressure fractionating column, and a liquid phase stream obtained from the column bottom of the low-pressure fractionating column is an alkylation oil product.

Abstract: The present invention relates to a method for obtaining a fraction oil yield from petroleum hydrocarbons in a distillation column, wherein said distillation column comprises a fractionation stage, a vaporization section and a stripping stage from the top to the bottom of the distillation column. The method comprises preheating and sending a feedstock oil of petroleum hydrocarbons through a pressure-feeding system at a pressure of 100-1000 kPa higher than the vaporization section pressure of the distillation column, wherein said preheating is conducted in a heating furnace, wherein said heating furnace has an outlet pressure of 100-1000 kPa higher than the vaporization section absolute pressure, and an outlet temperature of 360-460° C.

Abstract: A method for improving yield of petroleum hydrocarbon distillate in a distillation tower (6) comprises: preheating raw oil of petroleum hydrocarbon ready for fractionation; feeding it to a vaporization section (11) through a pressure feed system (3) under a pressure 100-1000 kPa higher than the vaporization section (11) of the distillation tower (6) for simultaneous atomizing and vaporizing; then feeding it to a fractionation section (13) for distillation-separation; and finally, discharging distillate product from the top and/or side of the tower and unvaporized heavy oil from the bottom. A distillation tower (6) for improving yield of petroleum hydrocarbon distillate comprises a vaporization section (11) and a fractionation section (13), and further comprises a pressure feed system (3) for feeding the raw oil of petroleum hydrocarbon ready for fractionation under a pressure 100-1000 kPa higher than that in the vaporization section (11) of the distillation tower (6).

Abstract: The present invention relates to a slurry bed loop reactor comprising a riser and at least one downcomer (3), wherein two ends of the riser are connected to two ends of the downcomer (3) via lines (16) and (7), respectively. The riser comprises a reaction section (1) and a settling section (2) with an increased tube diameter disposed on the reaction section (1). A gas outlet (13) exists at the top of the settling section (2). Each of the downcomers (3) is divided into a filtrate section (5) and a slurry section (6) by filter medium (4), wherein the filtrate section (5) is connected to a liquid outlet (10); two ends of the slurry section (6) are respectively connected to two ends of the riser, and the filtrate region (5) may further be connected to a back purging system.

Abstract: The present invention relates to a slurry bed loop reactor comprising a riser and at least one downcomer (3), wherein two ends of the riser are connected to two ends of the downcomer (3) via lines (16) and (7), respectively. The riser comprises a reaction section (1) and a settling section (2) with an increased tube diameter disposed on the reaction section (1). A gas outlet (13) exists at the top of the settling section (2). Each of the downcomers (3) is divided into a filtrate section (5) and a slurry section (6) by filter medium (4), wherein the filtrate section (5) is connected to a liquid outlet (10); two ends of the slurry section (6) are respectively connected to two ends of the riser, and the filtrate region (5) may further be connected to a back purging system.

Abstract: The present invention relates to a slurry bed loop reactor comprising a riser and at least one downcomer (3), wherein two ends of the riser are connected to two ends of the downcomer (3) via lines (16) and (7), respectively. The riser comprises a reaction section (1) and a settling section (2) with an increased tube diameter disposed on the reaction section (1). A gas outlet (13) exists at the top of the settling section (2). Each of the downcomers (3) is divided into a filtrate section (5) and a slurry section (6) by filter medium (4), wherein the filtrate section (5) is connected to a liquid outlet (10); two ends of the slurry section (6) are respectively connected to two ends of the riser, and the filtrate region (5) may further be connected to a back purging system.

Abstract: The present invention relates to a slurry bed loop reactor comprising a riser and at least one downcomer (3), wherein two ends of the riser are connected to two ends of the downcomer (3) via lines (16) and (7), respectively. The riser comprises a reaction section (1) and a settling section (2) with an increased tube diameter disposed on the reaction section (1). A gas outlet (13) exists at the top of the settling section (2). Each of the downcomers (3) is divided into a filtrate section (5) and a slurry section (6) by filter medium (4), wherein the filtrate section (5) is connected to a liquid outlet (10); two ends of the slurry section (6) are respectively connected to two ends of the riser, and the filtrate region (5) may further be connected to a back purging system.