China Petroleum & Chemical Corporation

Research Institute of Petroleum Processing, Sinopec

Other

Baoning Zong

Yibin Luo

Xuhong Mu

Xingtian Shu

Minggang Li

Xiaoxin Zhang

Enze Min

Xin Wang

Qiang Fu

Youhao Xu

Lin Cheng

Ying Ouyang

Junfeng Rong

Jingchuan Yu

Xuhua Zhou

Jinyu Zheng

Langyou Wen

Junying Zhu

Xugeng Huang

Ying Wang

Zheng Liu

Jun Long

Yong Xu

Hua Chen

Zhijian Da

Bo Zheng

Mingyuan He

Jianhong Gong

Bin Sun

Xuan Wang

Shouye Cui

Junyi Mao

Xiaojin Tang

Lifeng Hu

Zhenxing Zhu

Li Zhuang

Haiying Yang

Jinlian Tang

Wenhua Xie

Siyuan Qie

Zhiyong Pan

Keyong Yang

Dongqiang Ma

Dianzhong Wang

Jihong Zhou

Xiangkun Meng

Hailong Lin

Guohua Gao

Jianqi Fei

Minghui Dong

Weijia Wang

Bing Du

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

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.

Alkylation reaction apparatus, reaction system, and liquid acid catalyzed alkylation reaction process

The present invention provides a process of cultivating microalgae and a joint method of same jointed with denitration. During the microalgae cultivation, EM bacteria is added into the microalgae suspension. In the nutrient stream for cultivating microalgae, at least one of the nitrogen source, phosphorus source and carbon source is provided in the form of a nutrient salt. During the cultivation, the pH of the microalgae suspension is adjusted with nitric acid and/or nitrous acid. The joint method includes (1) a step of cultivating microalgae; (2) a separation step of separating a microalgae suspension obtained from step (1) into a wet microalgae (microalgae biomass) and a residual cultivation solution; and (3) a NOx absorbing/immobilizing step of denitrating an industrial waste gas with the residual cultivation solution obtained from step (2). The nutrient stream absorbed with NOx obtained from step (3) is used to provide nitrogen source to the microalgae cultivation of step (1).

Process of cultivating microalgae and a joint method of same with a denitration process

Disclosed is a process for producing light olefins, the process comprising: continuously contacting an oxygen-containing compound raw material with catalyst to have a dehydration reaction so as to prepare low-carbon alkene, the reaction pressure P of the dehydration reaction being 1-2 MPa, and the weight hourly space velocity H of the dehydration reaction being 15-50 h. The process of preparing light olefins has a simple and continuous operation process, reduces investment, greatly increases production of light olefins and has a high safety.

Process for producing light olefins

The present invention provides a joint method of cultivating microalgae combined with denitrating an industrial waste gas and a system useful for the same. The joint method comprises the steps of: (1) a step of cultivating microalgae; (2) a separation step of separating a microalgae suspension obtained from step (1) into a wet microalgae (microalgae biomass) and a residual cultivation solution; (3) a NOx absorbing/immobilizing step of denitrating an industrial waste gas with the residual cultivation solution obtained from step (2); wherein the nutrient stream absorbed with NOx obtained from step (3) is used to provide nitrogen source to the microalgae cultivation of step (1). During the microalgae cultivation, EM bacteria is added into the microalgae suspension. The microalgae is preferablysp.,sp.,sp. orsp.

Disclosed is a process for producing light olefins. In the process for producing light olefins by continuously bringing an alkane feedstock and a catalyst into contact to subject to a dehydrogenation reaction, the reaction pressure P of the dehydrogenation reaction is made 0.6-2 MPa and the volume space velocity H of the dehydrogenation reaction is made 500-1000 h. The light olefins production process of the present invention is simple and continuous in operation and has the characteristics of low investment, significant increase in yield of light olefins and high safety.

This invention relates to a process for co-producing cyclohexanol and alkanol, including a cyclohexene esterification step and a cyclohexyl ester hydrogenation step. This invention further relates to a process for further producing cyclohexanone or caprolactam, starting from the co-producing process, and an apparatus for co-producing cyclohexanol and alkanol. The process for co-producing cyclohexanol and alkanol of this invention is environment-friendly, with low production cost and highly improved atom economy.

Process and apparatus for co-producing cyclohexanol and alkanol

The present invention provides a process for preparing methanol, dimethyl ether, and low carbon olefins from syngas, wherein the process comprises the step of contacting syngas with a catalyst under the conditions for converting the syngas into methanol, dimethyl ether, and low carbon olefins, characterized in that, the catalyst contains an amorphous alloy consisting of a first component Al and a second component, said second component being one or more elements or oxides thereof selected from Group IA, IIIA, IVA, VA, IB, IIB, IVB, VB, VIB, VIIB, VIII, and Lanthanide series of the Periodic Table of Elements, and said second component being different from the first component Al. According to the present process, the syngas can be converted into methanol, dimethyl ether, and low carbon olefins in a high CO conversion, a high selectivity of the target product, and high carbon availability.

Process for preparing methanol, dimethyl ether, and low carbon olefins from syngas

The present invention provides a process for preparing methanol, dimethyl ether, and low carbon olefins from syngas, wherein the process comprises the step of contacting syngas with a catalyst under the conditions for converting the syngas into methanol, dimethyl ether, and low carbon olefins, characterized in that, the catalyst contains an amorphous alloy consisting of components M and X wherein the component X represents an element B and/or P, the component M represents two or more elements selected from Group IIIA, IVA, VA, IB, IIB, IVB, VB, VIB, VIIB, VIII and Lanthanide series of the Periodic Table of Elements. According to the present process, the syngas can be converted into methanol, dimethyl ether, and low carbon olefins in a high CO conversion, a high selectivity of the target product, and high carbon availability.

A modified zeolite beta having an anhydrous chemical formula, by weight % of the oxides, of (0-0.3)NaO.(0.5-10)AlO.(1.3-10)PO.(0.7-15)MO.(70-97)SiO, wherein M is one or more transition metal(s) selected from the group consisting of Fe, Co, Ni, Cu, Mn, Zn and Sn, x is the number of the atoms of said transition metal M, and y is a number that meets with the requirement of the oxidation state of said transition metal M, is disclosed. The modified zeolite beta can be used as an active component of a cracking catalyst or additive for catalytic cracking of petroleum hydrocarbons.

Modified zeolite beta

A MFI-structured molecular sieve containing phosphorus and metal components has a formula expressed in anhydrous form and on the basis of oxide weight, as follows: (0&#x2dc;0.3) NaO (0.5&#x2dc;5.5) AlO(1.3&#x2dc;10) PO(0.7&#x2dc;15) M1O(0.01&#x2dc;5) M2O(70&#x2dc;97) SiO, wherein M1 is one of transition metals selected from the group consisting of Fe, Co and Ni, and M2 is any one of metals selected from the group consisting of Zn, Mn, Ga and Sn. Preparation processes and uses of the instant molecular sieve are also provided. The molecular sieve has an excellent performance for increasing the yield of lower olefins and increasing the aromatics content in gasoline, and can be used as a shape-selective active component for the catalytic cracking catalyst of petroleum hydrocarbons or its additives.

Molecular sieve with MFI structure containing phosphorus and metal components, preparation process and use thereof

This invention relates to a composition with desulfurization property, in which the desulfurization component is a kind of molecular sieves with incorporation of vanadium into the skeleton. The composition has high hydrothermal stability and the vanadium is hard to lose.

Composition for desulfurization

A Y-zeolite-containing composite material made from materials comprising kaolin by in-situ crystallization, said composite material comprises nest-like structure. Content of Y-zeolite is in the range of 30&#x2013;85% by weight of said composite material. The nest-like structure is essentially comprised of rodlike crystal, further comprises flaky crystal or blocky crystal. Y-zeolite in the composite material may be HY, REY, or REHY. Said composite material is suitable to be used as catalysts for catalytic cracking of heavy oil or resid. The invention further relates to a process for preparing the composite material.

Y-zeolite-containing composite material and a process for preparing the same

A process for adsorptive desulfurization of gasoline or diesel oil or aromatics lower than Ccontaining organic sulfide impurities, wherein these feedstocks contact an amorphous alloy adsorbent comprising nickel as a major active component in a fluidized bed reactor or a magnetic-stabilized fluidized bed reactor or a slurry bed reactor. There is only a single diffuse peak at 2&#x3b8;=45&#xb0; in the 2&#x3b8; range from 20&#xb0; to 80&#xb0; in the X-ray diffraction (XRD) pattern of the adsorbent. The adsorbent consists of 50-95 wt % of nickel, 1-30 wt % of aluminum, 0-35 wt % of iron, and 0-10 wt % of one or more metals selected from copper, zinc, molybdenum, chromium, and cobalt.

Process for adsorptive desulfurization of light oil distillates

An amorphous alloy catalyst for hydrogenation and its preparation method are disclosed herein. The catalyst essentially consists of nickel ranging between 60 and 98 wt %, iron ranging between 0 and 20 wt %, one doping metal element selected from the group consisting of chromium, cobalt, molybdenum, manganese and tungsten ranging between 0 and 20 wt %, and aluminum ranging between 0.5 and 30 wt % based on the weight of said catalyst, wherein the weight percentages of iron and the doping metal element component may not be zero at the same time; and just one broad diffusion peak appears at about 2 &thgr;&equals;45&plusmn;1&deg; on the XRD patterns of the catalyst within 2 &thgr; range from 20 to 80&deg;. The catalyst herein can be used in processes for hydrogenation of unsaturated compounds such as olefin, alkyne, aromatics, nitro, carbonyl groups, nitrile and soon, and for hydrorefining of caprolactam in particular.

Hydrogenation catalyst and its preparation

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Beijing, China

Baoning Zong