Abstract: A supported catalyst has a support and a metal active component disposed on the support. The metal active component is at least one selected from the group consisting of a Group VIB metal element and a Group VIII metal element. The support contains at least one of heat-resistant inorganic oxides and molecular sieves and includes an internal channel penetrating the support. The ratio of the cross-section area of the channel to the cross-section area of the support is 0.05-3:100. The difference R between the water absorption rate and the BET pore volume of the support is not less than 0.2 mL/g. The supported catalyst can be used as a hydrogenation catalyst. When used in the hydrocracking of hydrocarbon oils, it can achieve high catalytic activity and high yield of jet fuels at the same time. The supported catalyst can also be used as a Fischer-Tropsch synthesis 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: The present invention provides an oil slurry filter, a filter unit including the oil slurry filter, a multiple-filter system including the oil slurry filter, and a multiple-stage filter system including the oil slurry filter. Due to the use of the filter component of flexible texture in the oil slurry filter of the present invention, the problems that the filter material is easily blocked by high-viscosity colloidal impurities, the regeneration efficiency of the filter is poor and the filtration efficiency is low are solved, and it is possible to make the backwash treatment of the filter residue more convenient and improve the regeneration efficiency of the filter. The present invention also provides a filtering process using the oil slurry filter to ensure long-term stable operation of the oil slurry filtering process.

Abstract: A modified ? zeolite has 0.5-15 wt % of an IVB group metal element in terms of oxide on the dry basis weight of the modified ? zeolite. The number of medium strong acid centers of the modified ? zeolite accounts for 30-60% of the total acid amount, the number of strong acid centers accounts for 5-25% of the total acid amount, and the ratio of B acid to L acid is 0.8 or more. The ratio of the weight content of the IVB group metal element in the modified ? zeolite body phase to the weight content of the IVB group metal element on the surface is 0.1-0.8. The catalytic cracking catalyst containing the modified ? zeolite has good selectivity and yield of C4 olefin.

Abstract: A catalytic conversion process for producing propylene includes the steps of: 1) providing a starting material comprising olefin(s) having 4 or more carbon atoms; 2) pretreating the starting material to obtain a propylene precursor comprising olefin(s) having 3×2n carbon atoms, wherein n is an integer greater than or equal to 1; and 3) subjecting the propylene precursor to a catalytic cracking reaction to obtain a reaction product comprising propylene.

Abstract: Disclosed are a phosphorus-containing high-silica molecular sieve, its preparation and application thereof, wherein the molecular sieve comprises about 86.5-99.8 wt % of silicon, about 0.1-13.5 wt % of aluminum and about 0.01-6 wt % of phosphorus, calculated as oxides and based on the dry weight of the molecular sieve, the molecular sieve has an XRD pattern with at least three diffraction peaks, the first strong peak is present at a diffraction angle of about 5.9-6.9°, the second strong peak is present at a diffraction angle of about 10.0-11.0°, and the third strong peak is present at a diffraction angle of about 15.6-16.7°. The phosphorus-containing high-silica molecular sieve shows an improved hydrocracking activity in the presence of nitrogen-containing species when used in the preparation of hydrocracking catalysts.

Abstract: In a method and system for treating a catalytic cracking gasoline, a catalytic cracking process, or a plant employs a fluidized reactor to carry out hydrodealkylation treatment on a catalytic cracking oil gas or catalytic cracking gasoline, so that heavy aromatics present therein can be efficiently converted into light olefins and light aromatics. The method and system can improve the yield of light olefins, allow a long-period stable operation, relieve the contradiction between supply and demand of light aromatics, and solve the problem of high content of heavy aromatics that have low value and are difficult to be utilized in aromatics present in oil gas from catalytic cracking units.

Abstract: The invention relates to a hydrocracking process and system. The gas oil feedstock and hydrogen are mixed and reacted in a hydrotreating unit. The resulting reaction effluent is sent to a first hydrogenation cracking unit and reacted by contacting a hydrogenation cracking catalyst I to obtain light fraction I rich in paraffins and heavy fraction I rich in cyclic hydrocarbons. The heavy fraction I is mixed with hydrogen and reacted in a second hydrogenation cracking unit, thereby producing heavy fraction II rich in cyclic hydrocarbons. The present invention wholly realizes the high-selective directional conversion of gas oil feedstock according to the chain structure and the ring structure and can produce chemical raw materials rich in paraffins and naphthenic speciality oil rich in cyclic hydrocarbons.

Abstract: The catalytic cracking catalyst contains a molecular sieve and an alumina substrate material. The alumina substrate material has a crystalline phase structure of ?-alumina. Based on the volume of pores with a diameter of 2-100 nm, the pore volume of the pores with a diameter of 2-5 nm accounts for 0-10%, the pore volume of the pores with a diameter of more than 5 nm and not more than 10 nm accounts for 10-25%, and the pore volume of the pores with a diameter of more than 10 nm and not more than 100 nm accounts for 65-90%.

Abstract: A lubricity modifier for fuels contain a dicarboxylic acid monoester compound represented by formula (I). In formula (I), R1 represents a single bond, a substituted or unsubstituted C2-6 divalent alkenyl group, or a group having a structure of —R3—R4—R5—; R2 represents a substituted or unsubstituted C1-40 hydrocarbyl group; R3 and R5 each independently represents a single bond, or a substituted or unsubstituted C1-3 divalent alkyl group; and R4 represents a substituted or unsubstituted C3-12 divalent alicyclic group.

Abstract: An organophosphorus compound has a structure represented by the general formula (I): The functional groups are defined in the description. The organophosphorus compound has prominent bearing capacity and excellent antiwear and antifriction performances, and can be used as an extreme pressure antiwear additive and used in lubricating oil and lubricating grease.

Abstract: A process for producing light olefins from inferior oils includes the steps of: subjecting an inferior oil to a thermal conversion reaction in the presence of hydrogen to obtain a conversion product; separating the conversion product to obtain a first separated product; separating the first separated product to obtain an upgraded oil and a pitch; subjecting the upgraded oil to hydro-upgrading to obtain a hydro-upgraded oil; separating the hydro-upgraded oil to obtain a hydro-upgraded heavy oil; and subjecting the hydro-upgraded heavy oil to catalytic cracking to obtain a catalytic cracking product comprising a light olefin.

Abstract: A method for producing light aromatics, includes the steps of: i) contacting a feedstock comprising heavy aromatic(s) with a catalyst in a fluidized reactor for aromatics lightening reaction in the presence of hydrogen to obtain a product rich in C6-C8 light aromatic(s) and a spent catalyst, wherein the heavy aromatic is one or more selected from C9+ aromatics; ii) separating the resulted product rich in C6-C8 light aromatic(s) to obtain hydrogen, a non-aromatic component, C6-C8 light aromatic(s) and a C9+ aromatic component; and iii) recycling at least a part of the C9+ aromatic component to the fluidized reactor. The method has strong adaptability to feedstocks and high flexibility in operation and allows a long-period stable operation. The method can produce high-value light aromatics from heavy aromatics that are difficult to be treated and utilized.

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 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 silole derivative is of formula (I): each of the groups in the above formula is defined as those in the description. The silole derivative of formula (I) has aggregation-induced emission performance, and is particularly applicable in luminescent parts and devices, fluorescent probes, biological imaging, lubricating oils and greases. A lubricating grease composition has photoluminescence performance, as well as one or more of advantageous anti-oxidation properties, anti-wear properties, extreme pressure properties and anti-rust properties. It is applicable in many mechanical equipment in electrical industry, metallurgical industry, food industry, paper industry, automobile industry and aircraft industry.

Abstract: A process for catalytic cracking of hydrocarbon oils includes the step of contacting a hydrocarbon oil feedstock with a catalytic cracking catalyst in a reactor comprising a dilute-phase transport fluidized bed and a fast fluidized bed connected in series for reaction. In the fast fluidized bed, the axial solid fraction ? of the catalyst is controlled within the range of about 0.1 to about 0.2. When used for catalytic cracking of hydrocarbon oil feedstocks, particularly heavy feedstock oils, the process and system show lower yields of dry gas and coke, and good product distribution.

Abstract: 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.