Abstract: Described are a process and a system for processing aromatics-rich fraction oil. The process includes: (1) introducing an aromatics-rich fraction oil into a fifth reaction unit for hydrosaturation, followed by fractionation, to provide a first light component and a first heavy component; (2) introducing a deoiled asphalt and an aromatics-comprising stream including the first heavy component into a hydrogen dissolving unit to be mixed with hydrogen, and introducing the mixed material into a first reaction unit for a hydrogenation reaction; (3) fractionating a liquid-phase product from the first reaction unit to provide a second light component and a second heavy component; (41) introducing the second light component into a second reaction unit for reaction; and (42) introducing the second heavy component into a delayed coking unit for reaction; or using the second heavy component as a component of low sulfur ship fuel oil.

Abstract: A frame rate changing method for an augmented reality device, including: obtaining scenario information of the augmented reality device, the scenario information comprising at least one of an external environment image, a virtual image, and an attitude parameter of the augmented reality device; when the scenario information changes, obtaining a target frame rate of the augmented reality device according to change information of the scenario information; and updating a frame rate of the augmented reality device according to the target frame rate, to display target content at the target frame rate. The present disclose realizes dynamic updating of the refresh frame rate of the augmented reality device, which is facilitate to reducing the system power consumption of the augmented reality device.

Abstract: The present application discloses a method for controlling a photographing function, which is applied to an AR apparatus, the method comprising: if a photographing function calling instruction is received, activating a photographing device of the AR apparatus; setting a display status of the AR apparatus to a non-preview status, wherein, a currently displayed content of the AR apparatus does not include a photographing preview content in the non-preview status; determining whether a photographing instruction is received; if so, controlling the photographing device to perform an operation corresponding to the photographing instruction. According to the present application, the power consumption of the photographing function of the AR apparatus can be reduced, and the endurance can be improved. The present application also discloses a device for controlling a photographing function, a storage medium and an AR apparatus which have the above beneficial effects.

Abstract: A catalyst has a carrier and a hydrogenation active metal component supported on the carrier. The hydrogenation active metal component contains at least one Group VIB metal component and at least one Group VIII metal component, and the carrier is composed of phosphorus-containing alumina. When the hydrogenation catalyst is measured using a hydrogen temperature programmed reduction method (H2-TPR), the ratio of the peak height of the low-temperature reduction peak, Plow-temp peak, at a temperature of 300-500° C. to the peak height of the high-temperature reduction peak, Phi-temp peak, at a temperature of 650-850° C., i.e. S=Plow-temp peak/Phi-temp peak, is 0.5-2.0; preferably 0.7-1.9, and more preferably 0.8-1.8. The hydrogenation catalyst shows excellent heteroatom removal effect and excellent stability when used in hydrotreatment.

Abstract: A molecular sieve has a silica/alumina molar ratio of 100-300, and has a mesopore structure. One closed hysteresis loop appears in the range of P/P0=0.4-0.99 in the low temperature nitrogen gas adsorption-desorption curve, and the starting location of the closed hysteresis loop is in the range of P/P0=0.4-0.7. The catalyst formed from the molecular sieve as a solid acid not only has a good capacity of isomerization to reduce the freezing point, but also can produce a high yield of the product with a lower pour point. The process for preparing the catalyst involves steps including crystallization, filtration, calcination, and hydrothermal treatment.

Abstract: Described are a process and a system for processing aromatics-rich fraction oil. The process includes: (1) introducing an aromatics-rich fraction oil into a fifth reaction unit for hydrosaturation, followed by fractionation, to provide a first light component and a first heavy component; (2) introducing a deoiled asphalt and an aromatics-comprising stream including the first heavy component into a hydrogen dissolving unit to be mixed with hydrogen, and introducing the mixed material into a first reaction unit for a hydrogenation reaction; (3) fractionating a liquid-phase product from the first reaction unit to provide a second light component and a second heavy component; (41) introducing the second light component into a second reaction unit for reaction; and (42) introducing the second heavy component into a delayed coking unit for reaction; or using the second heavy component as a component of low sulfur ship fuel oil.

Abstract: Described are a process and a system for hydrotreating a deoiled asphalt. The process includes: (2) introducing a deoiled asphalt and an aromatics-containing stream into a first reaction unit for hydrogenation reaction, wherein the first reaction unit comprises a mineral-rich precursor material and/or a hydrogenation catalyst, and the first reaction unit is a fixed bed hydrogenation unit; (21) fractionating the liquid-phase product from the first reaction unit to provide a first light component and a first heavy component; (31) introducing the first light component into a second reaction unit for reaction, to provide a gasoline component, a diesel component and/or a BTX feedstock component; and (32) introducing the first heavy component to a delayed coking unit for reaction; or using the first heavy component as a low sulfur ship fuel oil component.

Abstract: A molecular sieve has a silica/alumina molar ratio of 100-300, and has a mesopore structure. One closed hysteresis loop appears in the range of P/P0=0.4-0.99 in the low temperature nitrogen gas adsorption-desorption curve, and the starting location of the closed hysteresis loop is in the range of P/P0=0.4-0.7. The catalyst formed from the molecular sieve as a solid acid not only has a good capacity of isomerization to reduce the freezing point, but also can produce a high yield of the product with a lower pour point. The process for preparing the catalyst involves steps including crystallization, filtration, calcination, and hydrothermal treatment.

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 hydrocracking catalyst comprises a support, at least one of VIII Group metal components, and at least one of VIB Group metal components. The support comprises an acidic silica-alumina component and alumina derived from a pseudo-boehmite component, wherein the content of the acidic silica-alumina component is 3-80 wt %, the content of alumina derived from the pseudo-boehmite component is 20-95 wt %, based on the support. The support is obtained by mixing, molding, drying and calcining the acidic silica-alumina component with the pseudo-boehmite component, wherein said pseudo-boehmite component comprises pseudo-boehmite PB1 and pseudo-boehmite PB2, wherein the content of PB1 is 10-90 wt % and the content of PB2 is 0-60 wt % on a dry basis and based on the support.

Abstract: A hydrocracking catalyst comprises a support, at least one of VIII Group metal components, and at least one of VIB Group metal components. The support comprises an acidic silica-alumina component and alumina derived from a pseudo-boehmite component, wherein the content of the acidic silica-alumina component is 3-80 wt %, the content of alumina derived from the pseudo-boehmite component is 20-95 wt %, based on the support. The support is obtained by mixing, moulding, drying and calcining the acidic silica-alumina component with the pseudo-boehmite component, wherein said pseudo-boehmite component comprises pseudo-boehmite PB1 and pseudo-boehmite PB2, wherein the content of PB1 is 10-90 wt % and the content of PB2 is 0-60 wt % on a dry basis and based on the support.

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: Disclosed is a combined process for hydrotreating and catalytic cracking of residue, wherein the residue, catalytic cracking heavy cycle oil with acidic solid impurity being removed, optional distillate oil and adistillate of catalytic cracking slurry oil from which the acidic solid impurity is removed are fed into residue hydrotreating unit, the hydrogenated residue obtained and optional vacuum gas oil are fed into catalytic cracking unit to obtain various products; the catalytic cracking heavy cycle oil from which the acidic solid impurity is removed is circulated to the residue hydrotreating unit; the catalytic cracking slurry oil is separated by distilling, the distillate of the catalytic cracking slurry oil after removing off the acidic solid impurity is circulated to the residue hydrotreating unit.

Abstract: Disclosed is a combined process for hydrotreating and catalytic cracking of residue, wherein the residue, catalytic cracking heavy cycle oil with acidic solid impurity being removed, optional distillate oil and adistillate of catalytic cracking slurry oil from which the acidic solid impurity is removed are fed into residue hydrotreating unit, the hydrogenated residue obtained and optional vacuum gas oil are fed into catalytic cracking unit to obtain various products; the catalytic cracking heavy cycle oil from which the acidic solid impurity is removed is circulated to the residue hydrotreating unit; the catalytic cracking slurry oil is separated by distilling, the distillate of the catalytic cracking slurry oil after removing off the acidic solid impurity is circulated to the residue hydrotreating unit.

Abstract: A guard catalyst, comprising an alumina support and molybdenum and/or tungsten and nickel and/or cobalt supported on the alumina support, wherein the total ammonia integral adsorption heat of said alumina support does not exceed 25 J/g, the percentage taken up by the ammonia integral adsorption heat of the ammonia differential adsorption heat greater than 100 kJ/mol does not exceed 10% of the total ammonia integral adsorption heat. Compared to the catalysts of the prior art, the guard catalyst has higher catalytic activity, less coke deposit, lower reduction rate of pore volume, better stability of activity, and higher strength.

Abstract: A catalyst for hydrofining fraction oils, comprises an alumina carrier and at least one metal and/or thereof oxide of Group VIB and at least one metal and/or thereof oxide of Group VIII supported on said alumina carrier. The pore volume of said alumina carrier is not less than 0.35 ml/g, in which the pore volume of the pores having a diameter of 40-100 angstrom accounts for more than 80% of the total pore volume, the alumina carrier is prepared by a special process. The catalyst possesses relatively high hydrogenation activity.

Abstract: A guard catalyst, comprising an alumina support and molybdenum and/or tungsten and nickel and/or cobalt supported on the alumina support, wherein the total ammonia integral adsorption heat of said alumina support does not exceed 25 J/g, the percentage taken up by the ammonia integral adsorption heat of the ammonia differential adsorption heat greater than 100 kJ/mol does not exceed 10% of the total ammonia integral adsorption heat. Compared to the catalysts of the prior art, the guard catalyst has higher catalytic activity, less coke deposit, lower reduction rate of pore volume, better stability of activity, and higher strength.