China Petroleum & Chemical Corporation

Research Institute of Petroleum Processing, Sinopec

Sinopec Research Institute of Petroleum Processing Co., Ltd.

Yibin Luo

Xingtian Shu

Ying Ouyang

Jun Long

Xuhong Mu

Baoning Zong

Minggang Li

Jiushun Zhang

Youhao Xu

Xieqing Wang

Li Zhuang

Chaogang Xie

Yuxia Zhu

Jinyu Zheng

Qiang Fu

Huiping Tian

Zhijian Da

Yanfen Zuo

Genquan Zhu

Wenhua Xie

Enhui Xing

Xin Wang

Qiang Liu

Xue Yang

Jianqiang Liu

Xiaoxin Zhang

Yunpeng Zhang

Fei Ren

Beiyan Chen

Yihua Yang

Zhiguo Wu

Zhongqing Liu

Lina Zhou

Chengqiang Wang

Yueyang Han

Lingyin Du

Yong Xu

Bin Zhu

Zhenyu Chen

Hua Chen

Min Lin

Jianhong Gong

Mingyuan He

Mingde Xu

Wenbin Jiang

Shouye Cui

Chunfeng Shi

Yujian Liu

Haitao Song

Xuhui Bai

Jiasong Yan

Jinlian Tang

Langyou Wen

Zhiqiang Qiao

Jinghui Deng

Liuzhou Zhao

Youbao Lu

Yingchun Ru

Xiangtian Shu

Shaobing Yu

Chenghan Yan

Dianzhong Wang

Xiaojie Cheng

Minghui Dong

Weijia Wang

Zheng Li

Lisheng Li

Anguo Mao

Fengmei Zhang

Bing Du

A fluidized catalytic conversion method for producing light olefins includes the following steps: 1) introducing an olefin-rich feedstock into a fluidized catalytic conversion reactor, and contacting with a catalyst having a temperature of 650° C. or higher for reaction; 2) separating the reaction product vapor obtained by the reaction to obtain a stream comprising C5+ olefins; and 3) recycling at least a part of the stream comprising C5+ olefins to step 1) for further reaction. The fluidized catalytic conversion method can effectively improve the yield of light olefins, improve the selectivity and improve the ethylene/propylene ratio of the product.

Fluidized catalytic conversion method for preparing low-carbon olefins

A catalytic cracking agent has an active component consisting of a phosphorus-modified molecular sieve and a non-phosphorus-modified molecular sieve or only consisting of a phosphorus-modified molecular sieve. According to an electron probe microanalysis (EPMA), the D value of phosphorus in the catalytic cracking agent is ≥65%, preferably ≥68%, provided that the active component consists of the phosphorus-modified molecular sieve and the non-phosphorus-modified molecular sieve, or the D value of phosphorus in the catalytic cracking agent is ≥82%, preferably ≥84%, provided that the active component only consists of the phosphorus-modified molecular sieve.

Catalytic cracking agent containing phosphorus-modified molecular sieve, preparation process thereof, preparation system and use thereof

A phosphorus-modified MFI-structured molecular sieve is characterized in that the molecular sieve has a K value, satisfying: 70%≤K≤90%; for example, 75%≤K≤90%; further for example, 78%≤K≤85%. The K value is as defined in the specification. A cracking auxiliary or cracking catalyst contains the phosphorus-modified MFI molecular sieve.

Phosphorus-modified MFI-structured molecular sieve, catalytic cracking auxiliary and catalytic cracking catalyst containing phosphorus-modified MFI-structured molecular sieve, and processes for preparing the same

A fluidized catalytic conversion method for maximizing the production of propylene includes the steps of: 1) contacting a heavy feedstock oil with a catalytic conversion catalyst having a temperature of 650° C. or higher for reaction; 2) contacting a hydrocarbon oil feedstock having an olefin content of 50 wt % or more with the catalytic conversion catalyst after the reaction of step 1); 3) separating a first catalytic cracking distillate oil and a second catalytic cracking distillate oil from the resulting reaction products; 4) separating an olefin-rich stream from the first catalytic cracking distillate oil; and 5) recycling the olefin-rich stream. The method can effectively improve the yield of propylene and realize an effective utilization of petroleum resources.

Fluidized catalytic conversion method for maximizing production of propylene

A molecular sieve of MFI structure has a ratio of n(SiO2)/n(Al2O3) of more than 15 and less than 70. It has a content of phosphorus of 1-15 wt %, calculated as POand based on the dry weight of the molecular sieve and a content of the supported metal in the molecular sieve 1-10 wt % based on the oxide of the supported metal and the dry weight of the molecular sieve. The supported metal is one or two selected from lanthanum and cerium. The volume of mesopores in the molecular sieve represents 40-70% by volume of the total pore volume of the molecular sieve by volume, measured by a nitrogen adsorption BET specific surface area method, and the volume of mesopores means the pore volume of the pores having a diameter of more than 2 nm and less than 100 nm.

MFI structure molecular sieve rich in mesopore, preparation method therefor, and catalyst containing same and application thereof

A rare earth- and phosphorus-containing molecular sieve of MFI structure rich in mesopores has a ratio of n(SiO)/n(AlO) of more than 15 and less than 70. The molecular sieve has a content of phosphorus of 1-15 wt %, calculated as POand based on the dry weight of the molecular sieve. The content of the supported metal in the molecular sieve is 1-10 wt % supported metal M1 and 0.1-5 wt % supported metal M2 based on the oxide of the supported metal and the dry weight of the molecular sieve. The supported metal M1 is one or two selected from lanthanum and cerium, and the supported metal M2 is one selected from iron, cobalt, nickel, copper, manganese, zinc, tin, bismuth and gallium; the volume of mesopores in the molecular sieve represents 40-70% by volume of the total pore volume of the molecular sieve by volume.

Phosphorus-containing rare-earth-containing MFI structure molecular sieve rich in mesopore, preparation method, and catalyst containing same and application thereof

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

A catalytic conversion process for producing gasoline and propylene includes the steps of 1) subjecting a feedstock oil to a first catalytic conversion reaction in a first catalytic conversion reaction device to obtain a first reaction product; 2) separating the first reaction product to obtain a propylene fraction, a gasoline fraction and a fraction comprising Colefin; 3) carrying out an oligomerization reaction on the fraction comprising Colefin in an oligomerization reactor to obtain an oligomerization product comprising Colefin, and optionally separating the oligomerization product to obtain a fraction comprising Colefin; 4) recycling the Colefin-containing oligomerization product or fraction to the first catalytic conversion reaction device, and/or sending the Colefin-containing oligomerization product or fraction to a second catalytic conversion reaction device for a second catalytic conversion reaction to obtain a second reaction product comprising propylene.

Catalytic conversion process and system for producing gasoline and propylene

A catalytic cracking process includes a step of contacting a cracking feedstock with a catalytic cracking catalyst in the presence of a radical initiator for reaction under catalytic cracking conditions. The radical initiator contains a dendritic polymer and/or a hyperbranched polymer. The dendritic polymer and the hyperbranched polymer each independently has a degree of branching of about 0.3-1, and each independently has a weight average molecular weight of greater than about 1000. The catalytic cracking process is beneficial to enhancing and accelerating the free radical cracking of petroleum hydrocarbon and promoting the regulation of cracking activity and product distribution; by using the process disclosed herein, the conversion of catalytic cracking can be improved, the yields of ethylene and propylene can be increased, and the yield of coke can be reduced.

Catalytic cracking process and catalyst system therefor

A method for the treatment of silicon-containing wastewater from the preparation of a molecular sieve or a catalyst includes the step of contacting the silicon-containing wastewater with at least one acid or at least one alkali, so that at least a part of the silicon elements in the silicon-containing wastewater form a colloid. A mixture containing a colloid is thus obtained. A silicon-containing solid phase and a first liquid phase are produced by a solid-liquid separation. A solid phase and a second liquid phase are produced by a solid-liquid separation after at least a part of the metal elements in the first liquid phase form a precipitate. At least a part of the second liquid phase is subjected to electrodialysis to produce an acid liquor and/or an alkali liquor. The silicon-containing solid phase can be used as the raw material for a molecular sieve synthesis.

Preparation of molecular sieve and treatment of silicon-containing wastewater therefrom

The present application relates to a process for treating gasoline, comprising the steps of: contacting a gasoline feedstock with a mixed catalyst and subjecting it to desulfurization and aromatization in the presence of hydrogen to obtain a desulfurization-aromatization product; optionally, splitting the resulting desulfurization-aromatization product into a light gasoline fraction and a heavy gasoline fraction; and, optionally, subjecting the resulting light gasoline fraction to etherification to obtain an etherified oil; wherein the mixed catalyst comprises an adsorption desulfurization catalyst and an aromatization catalyst. The process of the present application is capable of reducing the sulfur and olefin content of gasoline and at the same time increasing the octane number of the gasoline while maintaining a high yield of gasoline.

Process for treating gasoline

A process for ion-exchanging an exchangeable-ion containing solid material, characterized in that said process include a bipolar membrane electrodialysis step, which comprises subjecting an aqueous ion-containing solution to a bipolar membrane electrodialysis to produce an acid liquid; an ion-exchange step, which comprises contacting the exchangeable-ion containing solid material with the acid liquid and conducting the ion-exchange to produce a slurry containing the ion-exchanged solid material; a solid-liquid separation step, which comprises subjecting the slurry containing the ion-exchanged solid material to a solid-liquid separation to produce a solid phase and a liquid phase, adjusting the liquid phase to a pH of 4-6.5, and subjecting the pH-adjusted liquid phase to a solid-liquid separation to produce a treatment liquid. Oxalic acid is used in at least one of the bipolar membrane electrodialysis step, the ion-exchange step, and the solid-liquid separation step.

Ion-exchange process

The present invention provides a rare earth-containing Y zeolite and a preparation process thereof, said rare earth-containing Y zeolite has a rare earth content as rare earth oxide of 10-25 wt %, a unit cell size of 2.440-2.472 nm, a crystallinity of 35-65%, a Si/Al atom ratio in the skeleton of 2.5-5.0; and a product of the ratio of the strength Iof the peak at 2&#x3b8;=11.8&#xb1;0.1&#xb0; to the strength Iof the peak at 2&#x3b8;=12.3&#xb1;0.1&#xb0; in the X-ray diffraction spectrogram of the zeolite and the weight percent of rare earth as rare earth oxide in the zeolite of higher than 48.

Rare earth-containing Y zeolite and a preparation process thereof

A modified Y-type molecular sieve has a unit cell size of 2.420-2.440 nm. It contains a phosphorus content of 0.05-6%, a REOcontent of 0.03-10%, and an alumina content of less than 22%, and a specific hydroxyl nest concentration of less than 0.35 mmol/g and more than 0.05 mmol/g. The modified Y-type molecular sieve is used as the active component in a catalytic cracking catalyst. The catalytic cracking catalyst maintains a stable activity for a long time, effectively controls the coke yield and increases the heavy oil utilization.

Modified Y-type zeolite and preparation process and use thereof

The present invention relates to a catalytic cracking catalyst and a preparation process thereof, the catalytic cracking catalyst has a cracking active component, an optional mesoporous aluminosilicate material, a clay and a binder, wherein said cracking active component comprises, substantially consists of or consists of: a rare earth-containing Y zeolite, an optional other Y zeolite, and an optional MFI-structured zeolite, said rare earth-containing Y zeolite has a rare earth content as rare earth oxide of 10-25 wt %, e.g. 11-23 wt %; a unit cell size of 2.440-2.472 nm, e.g. 2.450-2.470 nm; a crystallinity of 35-65%, e.g. 40-60%; a Si/Al atom ratio in the skeleton of 2.5-5.0; and a product of the ratio of the strength Iof the peak at 2&#x3b8;=11.8&#xb1;0.1&#xb0; to the strength Iof the peak at 2&#x3b8;=12.3&#xb1;0.1&#xb0; in the X-ray diffraction spectrogram of the zeolite and the weight percent of rare earth as rare earth oxide in the zeolite of higher than 48, e.g. higher than 55.

Catalytic cracking catalyst having a rare earth-containing Y zeolite and a preparation process thereof

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Beijing, China

Yibin Luo