Abstract: A system for producing needle coke and a method for producing needle coke using the system are provided. The system includes a coke tower, a pressure stabilization tower, a buffer tank and a coking fractionation tower. A pressure controller is provided at the top of the pressure stabilization tower for adjusting the pressure at the top thereof. An oil gas outlet of the coke tower is in communication with an oil gas inlet of the pressure stabilization tower through a pipeline. No pressure controller for adjusting the pressure at the top of the coke tower is provided in the coke tower or on the oil gas pipeline connecting the coke tower to the pressure stabilization tower.

Abstract: An apparatus, a process and a system for treating petroleum coke are provided. The apparatus includes an activation unit that is an annular furnace reactor. The system includes a first reactor, the apparatus as a second reactor, a washing and separating unit, a cooling unit, a dissolving and separating unit, a washing and drying unit, optionally a regenerating unit, optionally a drying and calcining unit and optionally an evaporation-crystallization unit. The process for producing carbon materials uses the system for treating petroleum coke. The apparatus, the process and the system can achieve continuous production, and have advantages of high activation efficiency and stable properties of the resultant carbon material products.

Abstract: A method for producing a fuel oil includes the steps of (1) bringing a sulfur-containing feedstock oil and an alkali metal into contact for a pre-reaction to obtain a pre-reaction material, wherein the pre-reaction is performed under hydrogen-free conditions; (2) bringing the pre-reaction material into contact with a hydrogen-supplying agent for a hydrogenation reaction; and (3) separating the material obtained in step (2) to obtain a liquid-phase product fuel oil and a solid mixture. Using this method, inferior and cheap feedstock oils, such as heavy residual oils, can be converted into fuel oils.

Abstract: A coking system comprises the 1st to the m-th heating units and the 1st to the n-th coke towers, each of the m heating units being in communication with the n coke towers, respectively, each of the n coke towers being in communication with one or more separation towers, respectively, in communication with the m-th heating unit and optionally with the i-th heating unit. The coking system can at least utilize petroleum series or coal series raw materials to produce high-quality needle coke with stable performance.

Abstract: A system for producing needle coke and a method for producing needle coke using the system are provided. The system includes a coke tower, a pressure stabilization tower, a buffer tank and a coking fractionation tower. A pressure controller is provided at the top of the pressure stabilization tower for adjusting the pressure at the top thereof. An oil gas outlet of the coke tower is in communication with an oil gas inlet of the pressure stabilization tower through a pipeline. No pressure controller for adjusting the pressure at the top of the coke tower is provided in the coke tower or on the oil gas pipeline connecting the coke tower to the pressure stabilization tower.

Abstract: The present invention relates to a solid precipitation apparatus and a solid precipitation process, wherein said apparatus and said process, particularly when used for the desalination of a high-salinity wastewater, can meet the requirement of stable operation for a long period, can realize efficient removal of salts from the wastewater, and solve the problems of difficult desalination of high-salinity wastewater, easy blockage, and the like. The solid precipitation apparatus comprises a housing, an inlet for a stream, a discharging outlet, and a support disposed in an inner chamber of said housing, wherein the configuration of said support is suitable for a solid substance to be deposited and loaded thereon.

Abstract: A pseudo-boehmite has a dry basis content of 55-85 wt % and contains a phosphoric acid ester group. The sodium oxide content is not greater than 0.5 wt %, and the phosphorus content (in terms of phosphorus pentoxide) is 1.2-5.7 wt %, relative to 100 wt % of the total weight of the pseudo-boehmite. The pseudo-boehmite has a low sodium content.

Abstract: A method for preparing hexadecahydropyrene includes the step of carrying out the hydrogenation reaction to hydrocarbon oil containing pyrene compounds in the presence of a hydrogenation catalyst. The pyrene compounds are selected from at least one of pyrene and unsaturated hydrogenation products thereof. The hydrogenation catalyst contains a carrier and an active metal component loaded on the carrier. The active metal component is Pt and/or Pd and the carrier contains a small crystal size Y zeolite, alumina and amorphous silica-alumina. The small crystal size Y zeolite has an average grain diameter of 200-700 nm, a molar ratio of SiO2 to Al2O3 of 40-120, a relative crystallinity of ?95%, and a specific surface area of 900-1,200 m2/g. The pore volume of secondary pores in 1.7-10 nm diameter is more than 50% of the total pore volume.

Abstract: A coking system comprises the 1st to the m-th heating units and the 1st to the n-th coke towers, each of the m heating units being in communication with the n coke towers, respectively, each of the n coke towers being in communication with one or more separation towers, respectively, in communication with the m-th heating unit and optionally with the i-th heating unit. The coking system can at least utilize petroleum series or coal series raw materials to produce high-quality needle coke with stable performance.

Abstract: A method for preparing hexadecahydropyrene includes the step of carrying out the hydrogenation reaction to hydrocarbon oil containing pyrene compounds in the presence of a hydrogenation catalyst. The pyrene compounds are selected from at least one of pyrene and unsaturated hydrogenation products thereof. The hydrogenation catalyst contains a carrier and an active metal component loaded on the carrier. The active metal component is Pt and/or Pd and the carrier contains a small crystal size Y zeolite, alumina and amorphous silica-alumina. The small crystal size Y zeolite has an average grain diameter of 200-700 nm, a molar ratio of SiO2 to Al2O3 of 40-120, a relative crystallinity of ?95%, and a specific surface area of 900-1,200 m2/g. The pore volume of secondary pores in 1.7-10 nm diameter is more than 50% of the total pore volume.

Abstract: A method of wax oil hydrocracking includes the steps of pre-hydrotreating wax oil to obtain a pre-hydrotreated material flow; controlling the pre-hydrotreated material flow and a hydrogen-containing material flow to contact with a first hydrocracking catalyst to obtain a first hydrocracked material flow, and dividing the first hydrocracked material flow into a first hydrocracked material flow A and a first hydrocracked material flow B; controlling the flow B and a hydrogen-containing material flow to contact with a second hydrocracking catalyst to obtain a second hydrocracked material flow, and then separating and fractionating the second hydrocracked material flow to obtain a hydrocracked tail oil product; controlling the flow A, at least a part of the hydrocracked tail oil product, and a hydrogen-containing material flow to contact with a hydrogenation isocracking catalyst to obtain a hydrogenation isocracked material flow, and then separating and fractionating the obtained hydrogenation isocracked material

Abstract: A method of wax oil hydrocracking includes the steps of pre-hydrotreating wax oil to obtain a pre-hydrotreated material flow; controlling the pre-hydrotreated material flow and a hydrogen-containing material flow to contact with a first hydrocracking catalyst to obtain a first hydrocracked material flow, and dividing the first hydrocracked material flow into a first hydrocracked material flow A and a first hydrocracked material flow B; controlling the flow B and a hydrogen-containing material flow to contact with a second hydrocracking catalyst to obtain a second hydrocracked material flow, and then separating and fractionating the second hydrocracked material flow to obtain a hydrocracked tail oil product; controlling the flow A, at least a part of the hydrocracked tail oil product, and a hydrogen-containing material flow to contact with a hydrogenation isocracking catalyst to obtain a hydrogenation isocracked material flow, and then separating and fractionating the obtained hydrogenation isocracked material

Abstract: Provided are a supported catalyst, a preparation method therefor and use thereof, and a method for the preparation of isobutylene from halomethane. The catalyst is characterized in that it comprises a carrier and a metallic active component supported on the carrier, wherein the metallic active component comprises zinc oxide and zinc halide. On the basis of the total amount of the catalyst, by weight content, the content of zinc oxide is 0.5%-20%, the content of zinc halide is 10%-50%, and the content of the support is 40%-88%. Compared with the prior art, the catalyst of the present invention can convert halomethane into isobutylene with a high selectivity. With the reaction for preparing of isobutylene by converting bromomethane according to the method of the present invention, the conversion of bromomethane is not less than 90% and the selectivity of isobutylene is not less than 80%.

Abstract: The present invention relates to a wet start-up method for hydrogenation unit, an energy-saving hydrogenation process, and a hydrogenation apparatus. The method involves heating a start-up activating oil to a specific temperature and flowing the heated oil through a bed of hydrogenation catalyst bed, so that the temperature at the catalyst bed layer is increased to 180±10° C. or above by means of heat exchange and the reaction heat generated from activation in the start-up method.

Abstract: Provided are a supported catalyst, a preparation method therefor and use thereof, and a method for the preparation of isobutylene from halomethane. The catalyst is characterized in that it comprises a carrier and a metallic active component supported on the carrier, wherein the metallic active component comprises zinc oxide and zinc halide. On the basis of the total amount of the catalyst, by weight content, the content of zinc oxide is 0.5%-20%, the content of zinc halide is 10%-50%, and the content of the support is 40%-88%. Compared with the prior art, the catalyst of the present invention can convert halomethane into isobutylene with a high selectivity. With the reaction for preparing of isobutylene by converting bromomethane according to the method of the present invention, the conversion of bromomethane is not less than 90% and the selectivity of isobutylene is not less than 80%.

Abstract: The present disclosure provides a reactor for at least two liquid materials, comprising an enclosed reactor housing; a feeding tube having liquid material inlets for receiving corresponding liquid materials respectively; a distribution tube communicating with the feeding tube and extending into the reactor housing, the distribution tube being provided with a plurality of distribution holes in the region thereof extending into the reactor housing; a rotating bed in form of a hollow cylinder, which is disposed in the reactor housing via a fixing mechanism, thus dividing inner cavity of the reactor housing into a central area and an outer area, the rotating bed being capable of rotating driven by a driving mechanism; and a material outlet provided in a lower portion of the reactor housing for outputting product after reaction.

Abstract: The present disclosure provides a reactor for at least two liquid materials, comprising an enclosed reactor housing; a feeding tube having liquid material inlets for receiving corresponding liquid materials respectively; a distribution tube communicating with the feeding tube and extending into the reactor housing, the distribution tube being provided with a plurality of distribution holes in the region thereof extending into the reactor housing; a rotating bed in form of a hollow cylinder, which is disposed in the reactor housing via a fixing mechanism, thus dividing inner cavity of the reactor housing into a central area and an outer area, the rotating bed being capable of rotating driven by a driving mechanism; and a material outlet provided in a lower portion of the reactor housing for outputting product after reaction.

Abstract: The present invention relates to a wet start-up method for hydrogenation unit, an energy-saving hydrogenation process, and a hydrogenation apparatus. The method involves heating a start-up activating oil to a specific temperature and flowing the heated oil through a bed of hydrogenation catalyst bed, so that the temperature at the catalyst bed layer is increased to 180±10° C. or above by means of heat exchange and the reaction heat generated from activation in the start-up method.

Abstract: The present invention relates to a hydrogenation catalyst composition, process for preparing the same and use thereof. The composition comprises a hydrogenation catalyst, an organonitrogen compound in an amount of 0.01%-20% by weight of the catalyst, a sulfiding agent in an amount of 30%-150% by weight of the sulfur-requiring amount calculated theoretically of the hydrogenation catalyst, and an organic solvent in an amount of 0.1%-50% by weight of the catalyst. The preparation process comprises introducing the required substances onto the hydrogenation catalyst in oxidation state. By introduction of the organonitrogen compound, sulfur and organic solvent, the hydrogenation catalyst composition of the present invention may further increase the sulfur-maintaining ratio of the catalyst during the activation, slow down the concentrative exothermic phenomenon, decrease the rate of temperature rise of the catalyst bed layer, and improve the activity of the catalyst.

Abstract: Disclosed are a mixed catalyst comprising catalyst A and catalyst B mixed in a volume ratio ranging from 1:0.1 to 1:10, heavy crude oil ebullated-bed hydrotreating systems comprising at least one ebullated-bed reactor comprising the mixed catalyst, and heavy crude oil ebullated-bed hydrotreating processes comprising: introducing heavy crude oil and hydrogen into at least one ebullated-bed reactor, reacting the heavy crude oil and the hydrogen with the mixed catalyst in the at least one ebullated-bed reactor to produce reaction products; and discharging the reaction products from the top of the at least one ebullated-bed reactor.