Abstract: 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 P2O5 and 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.

Abstract: A rare earth- and phosphorus-containing molecular sieve of MFI structure rich in mesopores has a ratio of n(SiO2)/n(Al2O3) of more than 15 and less than 70. The molecular sieve has a content of phosphorus of 1-15 wt %, calculated as P2O5 and 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.

Abstract: A solid acid catalyst has a macropore specific volume of about 0.30-0.50 ml/g, a ratio of macropore specific volume to specific length of catalyst particles of about 1.0-2.5 ml/(g·mm), and a ratio of specific surface area to length of catalyst particles of about 3.40-4.50 m2/mm. The macropore refers to pores having a diameter of more than 50 nm. An alkylation catalyst is based on the solid acid catalyst and can be used in alkylation reactions. The solid acid catalyst and alkylation catalyst show an improved catalyst service life and/or trimethylpentane selectivity when used in the alkylation of isoparaffins with olefins.

Abstract: A process for preparing a catalytic cracking catalyst includes steps of mixing raw materials including a rare earth-containing NaY molecular sieve obtained by contacting a NaY molecular sieve with a rare-earth salt solution or a mixed solution of rare-earth salt solution and ammonium salt solution, filtering, and water-washing, an inorganic oxide binder and a natural mineral, slurrying and shaping into shaped bodies; hydrothermally calcining shaped bodies in an atmosphere condition where a pressure is externally applied and an aqueous solution containing an acidic substance or an alkaline substance is externally added; and then ammonium-exchanging to remove the alkali metal. The present invention optimizes and shortens the preparation process of the catalyst, which can reduce the preparation cost, and the prepared catalyst has excellent heavy oil conversion ability, higher gasoline and diesel yield, lower coke selectivity, and relatively reduces the used amount of the molecular sieve in the catalyst.

Abstract: 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.

Abstract: 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.

Abstract: 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.

Abstract: 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 C4 olefin; 3) carrying out an oligomerization reaction on the fraction comprising C4 olefin in an oligomerization reactor to obtain an oligomerization product comprising C12 olefin, and optionally separating the oligomerization product to obtain a fraction comprising C12 olefin; 4) recycling the C12 olefin-containing oligomerization product or fraction to the first catalytic conversion reaction device, and/or sending the C12 olefin-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.

Abstract: A tin-titanium-silicon molecular sieve, a preparation method and an application thereof are provided. The electron binding energy of framework tin active centers in the tin-titanium-silicon molecular sieve is 488.5 eV or less. In the tin-titanium-silicon molecular sieve, the molar ratio of titanium to silicon is preferably 0.005-0.03, and the molar ratio of tin to silicon is preferably 0.005-0.025. The tin-titanium-silicon molecular sieve of the invention has more catalytic active centers, a lower electron binding energy of framework tin active centers, and an excellent catalytic performance.

Abstract: A phosphorus-containing or phosphorus-modified ZSM-5 molecular sieve is characterized in that in its 27Al MAS-NMR, the ratio of peak area for the resonance signal having a chemical shift of 39±3 ppm to peak area for the resonance signal having a chemical shift of 54 ppm±3 ppm is ?1; or in its surface XPS elemental analysis, the value of n1/n2 is ?0.1. n1 represents the mole number of phosphorus, n2 represents the total mole number of silicon and aluminum. A cracking auxiliary or cracking catalyst contains the phosphorus-containing/phosphorus-modified ZSM-5 molecular sieve can be made using the phosphorus-containing or phosphorus-modified ZSM-5 molecular sieve.

Abstract: 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.

Abstract: 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.

Abstract: A NaY molecular sieve with an aluminum-rich surface is prepared using a process that includes the steps of: a. mixing a directing agent and a first silicon source to obtain a first mixture, wherein the directing agent has a molar composition of Na2O:Al2O3:SiO2:H2O=(6-25):1:(6-25):(200-400); b. mixing the first mixture obtained in the step a with a second silicon source, an aluminum source and water to obtain a second mixture; c. carrying out hydrothermal crystallization on the second mixture obtained in the step b, and collecting a solid product. Calculated as SiO2, the weight ratio of the first silicon source to the second silicon source is 1:(0.01-12). The NaY molecular sieve has larger aluminum distribution gradient from the surface to the center of the particle than the conventional molecular sieve.

Abstract: A rare earth-containing Y zeolite has at least two mesopore pore-size distributions at 2-3 nanometers and 3-4 nanometers. A catalytic cracking catalyst contains the rare earth-containing Y zeolite. When used in the catalytic cracking of heavy oil, the catalytic cracking catalyst invention has excellent heavy oil conversion ability, higher gasoline yield, and lower coke selectivity.

Abstract: A rare earth-containing Y zeolite has at least two mesopore pore-size distributions at 2-3 nanometers and 3-4 nanometers. A catalytic cracking catalyst contains the rare earth-containing Y zeolite. When used in the catalytic cracking of heavy oil, the catalytic cracking catalyst provided has excellent heavy oil conversion ability, higher gasoline yield, and lower coke selectivity.

Abstract: 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 C4 olefin; 3) carrying out an oligomerization reaction on the fraction comprising C4 olefin in an oligomerization reactor to obtain an oligomerization product comprising C12 olefin, and optionally separating the oligomerization product to obtain a fraction comprising C12 olefin; 4) recycling the C12 olefin-containing oligomerization product or fraction to the first catalytic conversion reaction device, and/or sending the C12 olefin-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.

Abstract: A solid acid catalyst has a macropore specific volume of about 0.30-0.50 ml/g, a ratio of macropore specific volume to specific length of catalyst particles of about 1.0-2.5 ml/(g·mm), and a ratio of specific surface area to length of catalyst particles of about 3.40-4.50 m2/mm. The macropore refers to pores having a diameter of more than 50 nm. An alkylation catalyst is based on the solid acid catalyst and can be used in alkylation reactions. The solid acid catalyst and alkylation catalyst show an improved catalyst service life and/or trimethylpentane selectivity when used in the alkylation of isoparaffins with olefins.

Abstract: 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.

Abstract: A rare earth- and phosphorus-containing molecular sieve of MFI structure rich in mesopores has a ratio of n(SiO2)/n(Al2O3) of more than 15 and less than 70. The molecular sieve has a content of phosphorus of 1-15 wt %, calculated as P2O5 and 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.

Abstract: 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 P2O5 and 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.