Abstract: The present invention relates to a hydrocracking catalyst comprising an acidic silica-alumina, an optional alumina, an effective quantity of at least one VIII Group metal component(s), an effective quantity of at least one VIB Group metal component(s) and an organic additive, wherein the organic additive is one or more selected from the group consisting of an oxygen-containing or nitrogen-containing organic compound, and the molar ratio of the organic additive to the VIII Group metal component(s) is 0.01-10. The present invention relates further to a process for producing the hydrocracking catalyst and use of the catalyst in a process for hydrocracking hydrocarbon oils. The hydrocracking catalyst provided according to the present invention shows a higher activity for aromatic hydrosaturating and ring-opening reaction, as compared with the prior art hydrocracking catalyst.

Abstract: A process for producing an alkylene oxide by olefin epoxidation, wherein said process comprises the steps of: (1) in a first olefin epoxidation condition, in the presence of a first solid catalyst, a first mixed stream containing a solvent, an olefin and H2O2 is subjected to an epoxidation in one or more fixed bed reactors and/or one or more moving bed reactors until the conversion of H2O2 reaches 50%-95%, then, optionally, the resulting reaction mixture obtained in the step (1) is subjected to a separation to obtain a first stream free of H2O2 and a second stream containing the unreacted H2O2, and the olefin is introduced to the second stream to produce a second mixed stream, or optionally, the olefin is introduced to the reaction mixture obtained in the step (1) to produce a second mixed stream; (2) in a second olefin epoxidation condition, the reaction mixture obtained in the step (1) or the second mixed stream obtained in the step (1) and a second solid catalyst are introduced to one or more slurry bed re

Abstract: A process for producing light olefins and aromatics, which comprises reacting a feedstock by contacting with a catalytic cracking catalyst in at least two reaction zones, wherein the reaction temperature of at least one reaction zone among the reaction zones downstream of the first reaction zone is higher than that of the first reaction zone and its weight hourly space velocity is lower than that of the first reaction zone, separating the spent catalyst from the reaction product vapor, regenerating the separated spent catalyst and returning the regenerated catalyst to the reactor, and separating the reaction product vapor to obtain the desired products, light olefins and aromatics. This process produces maximum light olefins such as propylene, ethylene, etc from heavy feedstocks, wherein the yield of propylene exceeds 20% by weight, and produces aromatics such as toluene, xylene, etc at the same time.

Abstract: The present invention relates to a catalyst for converting inferior acid-containing crude oil. Based on the total amount of the catalyst, said catalyst comprises from 1 to 50 wt % of a mesopore material, from 1 to 60 wt % of molecular sieves and from 5 to 98 wt % of thermotolerant inorganic oxides and from 0 to 70 wt % of clays. Said mesopore material is an amorphous material containing alkaline earth oxide, silica and alumina, and has an anhydrous chemical formula of (0-0.3)Na2O.(1-50)MO.(6-58)Al2O3.(40-92)SiO2, based on the weight percent of the oxides, wherein M is one or more selected from Mg, Ca and Ba. Said mesopore material has a specific surface area of 200-400 m2/g, a pore volume of 0.5-2.0 ml/g, an average pore diameter of 8-20 nm, and a most probable pore size of 5-15 nm. The catalyst provided in the present invention is suitable for the catalytic conversion of crude oil having a total acid number of greater than 0.

Abstract: The present invention relates to a process for simulated moving bed (SMB) adsorption and separation with a reduced number of control valves, comprising separating the feedstocks comprising isomers by SMB adsorption, said SMB comprising m beds of adsorbent, each of which is equipped with grids, each of the grids being equipped with the materials charging and discharging pipeline of the bed, the materials charged into and discharged from SMB at least comprising adsorption feedstocks, desorbent, extract, raffinate and the flushing liquids charged from different beds, wherein the to extract is enriched with the target product; there are at least two streams of said flushing liquid selected from any one of the adsorption feedstock, desorbent, extract and raffinate; there are altogether n streams of materials charged to and discharged from the SMB, wherein there are s types of materials having the same composition and flow direction; p sets of on-off valves are used to control n streams of materials is charged to a

Abstract: The object of the present invention is to provide a catalyst regeneration process which can improve catalyst selectivity. A first aspect of the invention is characterized in that a spent catalyst from a reactor is introduced into a first fluidized bed regenerator and contacted with an oxygen-containing gas stream and optional steam to carry out a coke combustion reaction, wherein the resultant mixture of the partially regenerated catalyst and flue gas is introduced into a second fluidized bed regenerator and contacted with steam and an optional oxygen-containing gas stream to carry out a further regeneration reaction, and then the regenerated catalyst is introduced into the reactor. A second aspect of the invention is characterized in that a spent catalyst from a reactor is introduced into a fluidized dense bed regenerator and contacted with an oxygen-containing gas stream and steam to carry out a coke combustion reaction, and then the regenerated catalyst is introduced into the reactor.

Abstract: An agglomerated zeolite adsorbent which comprises 95-99.5 mass % of X zeolite and 0.5-5.0 mass % of binder, wherein the exchangeable cationic sites of said X zeolite are occupied by Group IIA metal and/or K, the total pore volume of said adsorbent is no less than 0.26 mL/g as measured by mercury porosimetry, the volume of pores with pore diameters from 100 to 500 nm is at least 60% based on the total pore volume. During shaping, a pore-forming agent is added to this adsorbent, and then the adsorbent is alkali treated for in-situ crystallization, followed by ion exchange. Said adsorbent has high adsorption capacity, fast mass transfer rate and good mechanical strength. Said adsorbent is suitable for liquid phase adsorptive separation of para-xylene from C8 aromatic hydrocarbons and is also suitable for adsorptive separation of other alkyl aromatic hydrocarbons isomers.

Abstract: A process for producing light olefins and aromatics, which comprises reacting a feedstock with a catalytic cracking catalyst in at least two reaction zones, wherein the reaction temperature of at least one reaction zone downstream of the first reaction zone is higher than that of the first reaction zone and its weight hourly space velocity is lower than that of the first reaction zone. The spent catalyst is separated, from the reaction product vapor, regenerated, and then returned to the reactor. The reaction product vapor is separated to obtain the desired products, light olefins and aromatics. This process efficiently produces light olefins such as propylene, ethylene, etc from heavy feedstocks, wherein the yield of propylene exceeds 20% by weight, and produces aromatics such as toluene, xylene, etc at the same time.

Abstract: This disclosure provides an adsorbing agent which, on the basis of the total weight of the adsorbing agent, comprises the following components: 1) a Si—Al molecular sieve having a BEA structure, in an amount of 1-20 wt %, 2) at least one binder selected from the group consisting of titanium dioxide, stannic oxide, zirconium oxide and alumina, in an amount of 3-35 wt %, 3) a silica source, in an amount of 5-40 wt %, 4) zinc oxide, in an amount of 10-80 wt %, and 5) at least one promoter metal selected from the group consisting of cobalt, nickel, iron and manganese, based on the metal, in an amount of 5-30 wt %, wherein at least 10 wt % of the promoter metal is present in a reduced valence state. The adsorbing agent exhibits improved activity and stability, and at the same time, is capable of significantly improving the octane number of the product gasoline.

Abstract: A hydrocarbon conversion catalyst, which comprises, based on the total weight of the catalyst, 1-60 wt % of a zeolite mixture, 5-99 wt % of a thermotolerant inorganic oxide and 0-70 wt % of clay, wherein said zeolite mixture comprises, based on the total weight of said zeolite mixture, 1-75 wt % of a zeolite beta modified with phosphorus and a transition metal M, 25-99 wt % of a zeolite having a MFI structure and 0-74 wt % of a large pore zeolite, wherein the anhydrous chemical formula of the zeolite beta modified with phosphorus and the transition metal M is represented in the mass percent of the oxides as (0-0.3)Na2O.(0.5-10)Al2O3.(1.3-10)P2O5.(0.7-15)MxOy.(64-97)SiO2, in which the transition metal M is one or more selected from the group consisting of Fe, Co, Ni, Cu, Mn, Zn and Sn; x represents the atom number of the transition metal M, and y represents a number needed for satisfying the oxidation state of the transition metal M.

Abstract: The present invention relates to an airflow particle sorter, comprising: a top-sealed sorter main body, a discharge port, an outtake tube and at least one directing-intake port; the inner space of the sorter main body, from the above to the bottom, includes, a straight tube zone and a cone zone, the conical bottom of the cone zone is connected to the straight tube zone; the discharge port is located at the bottom of the cone zone; the directing-intake port is installed in the upper part of the straight tube zone in a tangential direction of the straight tube zone, and is communicated with the inner space of the sorter main body; the outtake tube is hermetically inserted into the top of the sorter main body, and extends downwardly to the lower part of the straight tube zone, and the outtake tube has a sealed bottom end; the lower part of the outtake tube is installed with at least one directing-outtake port, which communicates the outtake tube with the inner space of the sorter main body, the directing-outtake

Abstract: The present invention provides a hydrogenation catalyst, containing a carrier, metal components of nickel, molybdenum and tungsten supported thereon, and an adjuvant component selected from the group consisting of fluorine and phosphor and combination thereof. In another embodiment, the present invention provides a hydrogenation catalyst, containing a carrier and metal components of nickel, molybdenum and tungsten supported thereon, wherein said carrier contains a molecular sieve. The present invention provides further use of said catalyst in the process for hydrogenating hydrocarbon oil. In comparison with a hydrogenation catalyst according to the prior art, the catalyst according to the present invention has a much higher activity.

Abstract: The present invention relates to an organic molybdenum additive and its preparation method, and a lubricating composition comprising said additive, and use of said additive and its lubricating composition in the aspect of improving antiwear and antifriction property of oil products. The organic molybdenum additive according to the present invention is characterized in that it is prepared by reacting several kinds of feedstock as follows: a polylol ester of p-hydroxybenzene alkyl acid, an inorganic molybdenum compound and an aliphatic amine and/or an aromatic amine and/or an amide. The organic molybdenum additive of the present invention has excellent antiwear and/or antifriction property.

Abstract: 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 I1 of the peak at 2?=11.8±0.1° to the strength I2 of the peak at 2?=12.3±0.1° 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.

Abstract: The present invention relates to a method for processing a sulfur-containing gas and a hydrogenation catalyst used therefor. The method comprises introducing the sulfur-containing gas into the tail gas hydrogenation unit of a sulfur recovery device, processing it with the hydrogenation catalyst of the present invention, and absorbing the hydrogenated tail gas with a solvent. The hydrogenation catalyst comprises from 0.5 to 3 wt. % of an active component nickel oxide, from 1 to 4 wt. % of an active component cobalt oxide, from 8 to 20 wt. % of an active component molybdenum oxide or tungsten oxide, from 1 to 5 wt. % of a deoxidation auxiliary agent, from 10 to 40 wt. % of TiO2, the balance being ?-Al2O3, based on the weight of the catalyst.

Abstract: 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.

Abstract: The invention discloses a catalyst and a method for cracking hydrocarbons. The catalyst comprises, calculated by dry basis, 10˜65 wt % ZSM-5 zeolite, 0˜60 wt % clay, 15˜60 wt % inorganic oxide binder, 0.5˜15 wt % one or more metal additives selected from the metals of Group VIIIB and 2˜25 wt % P additive, in which the metal additive is calculated by metal oxide and the P additive is calculated by P2O5. The method for cracking hydrocarbons using this catalyst increases the yield of FCC liquefied petroleum gas (LPG) and the octane number of FCC gasoline, as well as it increases the concentration of propylene in LPG dramatically.

Abstract: The present invention discloses a catalytic cracking catalyst and a preparation process therefor. The catalytic cracking catalyst comprises a cracking active component, 10 wt %-70 wt % of a clay on the dry basis, and 10 wt %-40 wt % of an inorganic oxide binder (as oxide), relative to the weight of the catalytic cracking catalyst, wherein said cracking active component contains, relative to the weight of the catalytic cracking catalyst, 10 wt %-50 wt % of a modified Y-type zeolite on the dry basis and 0-40 wt % of other zeolite on the dry basis, wherein said modified Y-type zeolite is characterized by having a unit cell size of 2.420-2.440 nm; as percent by weight of the modified Y-type zeolite, a phosphorus content of 0.05-6%, a RE2O3 content of 0.03-10%, and an alumina content of less than 22%; and a specific hydroxy nest concentration of less than 0.35 mmol/g and more than 0.05 mmol/g.

Abstract: The present invention relates to a catalyst combination for hydrotreating raw oils and a process for hydrotreating raw oils with the catalyst combination. The catalyst combination comprises one or both of at least one hydrogenation protection catalyst I and at least one hydrogenation demetalling catalyst I; at least one hydrogenation demetalling catalyst II; and at least one hydrogenation treatment catalyst III.

Abstract: A catalytic conversion process for increasing the light olefin yields, which comprises bringing a hydrocarbon oil feedstock into contact with a catalytic conversion catalyst in a catalytic conversion reactor including one or more reaction zones to carry out the reaction, wherein the hydrocarbon oil feedstock is subjected to the catalytic conversion reaction in the presence of an inhibitor; and separating the reactant vapor optionally containing the inhibitor from the coke deposited catalyst, wherein a target product containing ethylene and propylene is obtained by separating the reactant vapor, and the coke deposited catalyst is stripped and regenerated for recycle use by being returned to the reactor. The process can weaken the further converting reaction of produced light olefins such as ethylene and propylene to 50-70% of the original level by injecting the inhibitor; thereby it can increase the yields of the target products.