China Petroleum & Chemical Corporation

Research Institute of Petroleum Processing, Sinopec

Tsinghua University

Zhenxing Zhu

Junyi Mao

Xiaojin Tang

Lifeng Hu

Yongxiang Li

Zhihai Zhao

Zheng Liu

Tao Huang

Qing Yuan

Bo Zheng

Baoning Zong

Jun Gao

Shuandi Hou

Kejia Xu

Fei Wei

Zhanzhu Zhang

Siyuan Qie

Hongliang Qu

Zhiyong Pan

Shaobing Wang

Silei Sun

Guohua Gao

Jianqi Fei

Ya Qin

Tongwang Zhang

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.

Method for separating 2-alkylanthracenes and use thereof for producing hydrogen peroxide

The present disclosure generally relates to a liquid-solid radial moving bed reaction apparatus comprising a radial moving bed reactor, a spent catalyst receiver, a catalyst regenerator, and a regenerated catalyst receiver that are successively connected. Also disclosed is a solid acid alkylation process using the liquid-solid radial moving bed reaction apparatus.

Liquid-solid radial moving bed reaction device and solid acid alkylation method

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 (), a spent catalyst receiver (), a catalyst regenerator () and a regenerated catalyst receiver () that are successively connected, wherein, a catalyst outlet of the regenerated catalyst receiver () is communicated with a catalyst inlet of the axial moving bed reactor (); Wherein, the axial moving bed reactor () is provided with at least two catalyst beds () arranged up and down, the axial moving bed reactor () is provided with a feed inlet () above each catalyst bed (); A catalyst delivery pipe () is arranged between two adjacent catalyst beds () so that the catalyst can move from top to bottom in the axial moving bed reactor (); A separation component () is provided between two adjacent catalyst beds (), the inside space of the separation component () is communicated with the catalyst delivery pipe (), the separation component () 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 () moves down through the catalyst delivery pipe ().

Liquid-solid axial moving bed reaction and regeneration device, and solid acid alkylation method

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&#xb0; C.-150&#xb0; 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.

Process for separating alkylation product, alkylation reaction and separation process, and related apparatus

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.

This disclosure relates to the technical field of carbon nanotubes, provides an ultra-long chiral carbon nanotube and a method for preparing the same. The ultra-long chiral carbon nanotube has a diameter of about 1.5 nm to 5.5 nm and has a length of about 100 mm to 650 mm, the ultra-long chiral carbon nanotube includes a double-walled carbon nanotube and a triple-walled carbon nanotube, and each layer of the ultra-long chiral carbon nanotube is semiconducting and has a helix angle greater than 10&#xb0;.

Ultra-long chiral carbon nanotube, method for preparing the same, application thereof, and high-performance photoelectric device

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&#xb0; C.

Distillation tower for improving yield of petroleum hydrocarbon distillate and feeding method thereof

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Beijing, China

Zhenxing Zhu