70results about How to "Less coke" patented technology

The catalyst for residual oil hydrocracking in suspension bed is prepared with molybdenum ore dressing tailing or slag as material, and through wet oxidation and leaching with chemical reagent, filtering and other processing steps to obtain solution being used as the catalyst for hydrocracking in suspension bed. The catalyst is dispersed in heavy oil or residual oil, and in the presence of hydrogen, the inferior heavy oil or residual oil containing the catalyst is hydrocracked into light product. The catalyst has the features of low cost, environment friendship, high light product yield and others.

The present invention provides a pyrolysis tube for enhancing the yield of olefins and reducing a coking tendency in steam cracking of hydrocarbons. According to the present invention, the pyrolysis tube is characterized in that a plurality of mixing blades made by twisting two ends of a plate in opposite directions are included therein. The yield of ethylene is thereby improved and the coking tendency is reduced by mixing a fluid flow, improving a heat transfer rate and shortening a residence time of the reactants therein.

A method and apparatus for converting a hydrocarbon and oxygen containing gas feed stream to a product stream, such as syngas, including catalytically partially oxidizing the hydrocarbon feed stream over a catalyst bed. The catalyst bed has a downstream zone which is less resistant to flow than the upstream zone.

The invention provides heavy oil coking equipment, which includes a heating furnace (a), a coke reactor (b), a spray coking tower (c), a cyclone separator (d) and a fractionating tower (e). A coking raw material is preheated in a heating furnace (a) and then atomized by an atomizing nozzle (c18) of the spray coking tower (c), oxygen-containing high temperature gas from the heating furnace (a) is deoxidized by the coke reactor (b) and then contacts the atomized state coking raw material in the spray coking tower (c) to carry out coking reaction, the coarse coke powder in the coking reaction product is collected from a lower cone collection area (c22), oil gas and coke fine powder in the coking reaction product are separated by the cyclone separator (d), and oil gas is introduced into the fractionating tower (e) to perform fraction separation. Belonging to direct heating type coking equipment, the heavy oil coking equipment can greatly reduce coking in a heating furnace tube and improve the liquid yield, also the obtained coke powder and the dry gas from the fractionation tower can be burnt to serve as the heat source of the heavy oil coking equipment.

The invention provides a heavy oil coking method including the steps of: 1) atomizing a heavy oil coking raw material at 50-400 DEG C; 2) contacting the atomized heavy oil coking raw material with deoxidized flue gas at 490-750 DEG C to enable the atomized heavy oil coking raw material to reach a coking temperature, so that a coking reaction can be carried out; 3) separating coke coarse powder, coke fine powder and oil gas from a coking reaction product; and 4) performing fraction separation to the oil gas. The heavy oil coking method not only reduces, even completely avoids coking in a furnace tube of a heating furnace and increases liquid yield, but also is free of steps of desulfurization, denitrification and dust removal to the flue gas, so that the method is free of a large quantity of decoking waste water generated in coking and has a great industrial application prospect.

The invention provides a residual oil hydrocracking method, which adopts a tube-in-tube reactor, and a gas-liquid separator is arranged on the top of the inner tube. The separator is separated, the gas phase is discharged from the reactor, and the liquid phase enters the loop reaction section together with the added hydrocarbon oil containing more heavy aromatics, and at the same time hydrogen is added at the bottom of the loop reaction section. Compared with the prior art, the method of the invention has the advantages of uniform reactor temperature, less coke deposition, reduced dry gas output and the like. The method of the invention is mainly applicable to the hydrocracking reaction of heavy and residual oil, especially the hydrocracking reaction of inferior heavy and residual oil.

A method and apparatus for converting a hydrocarbon and oxygen containing gas feed stream to a product stream, such as syngas, including catalytically partially oxidizing the hydrocarbon feed stream over a catalyst bed. The catalyst bed has a downstream zone which is less resistant to flow than the upstream zone.

A two-way combined process of wax oil hydro-process and catalytic crack is carried out by entering wax oil, catalytic cracking re-circulating oil and catalytic cracking diesel oil into hydro-processor, hydrogenation reacting under existence of hydrogen and hydrogenation catalyst, separating for reactant to obtain gas, hydrogenation naphtha oil, hydrogenation diesel oil and hydrogenation tail oil, entering hydrogenation tail oil into catalytic cracker, crack reacting under existence of catalytic cracking agent, separating to obtain dry gas, liquefied gas, catalytic cracking gasoline, catalytic cracking diesel oil and catalytic cracking re-circulating oil and oil slurry, and circulating for catalytic cracking diesel oil and catalytic cracking re-circulating oil to hydro-processor. It has higher recovery rate and cetyl value, less sulfur content, arene content and coke output.

The invention provides a heavy oil hydro-conversion method. The method comprises the following steps that: (1) heavy oil or heavy oil and hydrogen enter a first reactor to be subjected to a hydrogen-thermal cracking reaction in the presence or absence of a hydrogen-thermal cracking catalyst; (2) deoiled asphalt, a hydrogen-thermal cracking catalyst and hydrogen enter a second reactor, contact with the hydrogen-thermal cracking catalyst, and are subjected to a hydrogen-thermal cracking reaction at a relatively low temperature; (3) the reaction product in the first reactor and the reaction product of the second reactor are mixed and enter a separation unit, and are separated to obtain a distillate product and residual oil; and (4) the residual oil from the step (3) enters a solvent extraction tower to remove asphalt to obtain deasphalted oil and deoiled asphalt, and the deoiled asphalt is returned to the second reactor for further reacting, wherein the reacting temperature of the second reactor is 5-50 DEG C lower than that of the first reactor. Compared with the prior art, the method has the advantages of remarkably improving the heavy oil conversion rate and light oil yield, and improving the light rate of heavy oil.

Two-stage heavy oil slurry-bed reactor hydrogenation equipment and a method thereof are disclosed. The equipment comprises a first slurry-bed reactor, a first separating unit communicated with the first slurry-bed reactor, a second slurry-bed reactor communicated with a discharge port of the first separating unit, and a second separating unit communicated with the second slurry-bed reactor. The first and second slurry-bed reactors comprise a riser tube (1) and a downcomer (8). Upper parts and lower parts of the riser tube (1) and the downcomer (8) are respectively communicated through connecting pipes. An opening of the upper connecting pipe (7) extends into the lower part of the downcomer (8). The bottom of the riser tube (1) is provided with a raw material inlet. Tops of the riser tube (1) and the downcomer (8) are respectively provided with gas outlets. The middle upper part of the downcomer (8) is provided with a product outlet. The two-stage heavy oil slurry-bed reactor hydrogenation equipment and the method are convenient for long-term operation of the reactors, hydrogenation conversion rate of heavy oil is raised, and slurry processing of subsequent equipment is enhanced.

The invention provides a catalytic hydroprocessing thermal cracking catalyst, a preparation method thereof and a composite catalyst for producing high-density fuel blending components by inferior heavy oil hydroprocessing. The catalyst takes silicon dioxide as an inner core, and molybdenum disulfide is coated outside the inner core to serve as a shell; and the catalyst is prepared by enabling an ethanol dispersion solution of ammonium tetrathiomolybdate and silicon dioxide, serving as a raw material, to react with an amphipathic molecule modifying agent under the participation of hydroxylamine hydrochloride serving as a reducing agent. The composite catalyst comprises the catalytic hydroprocessing thermal cracking catalyst and a fixed-bed hydrogenation catalyst. The catalyst is applied to the slurry-bed hydrocracking technology of inferior residual oil, the addition amount of the catalyst can be reduced, and the processing cost of the residual oil can be lowered.

The invention discloses a desulphurization catalyst, a preparation method of the desulphurization catalyst and the desulphurization catalyst obtained by the method, and an application of the desulphurization catalyst in sulfur-containing hydrocarbon oil desulphurization. The desulphurization catalyst contains alumina, a silicon oxide source, a first metal oxide, antimony oxide, a rare-earth metal oxide and active metal; and an XRD spectrum of the desulphurization catalyst has a characteristic peak of a rare earth-antimony composite oxide. The desulphurization catalyst has better desulphurization activity and activity stability.

The invention provides a heavy oil hydro-conversion method. The method comprises the following steps: (1) a heavy oil raw material and heavy wax oil enter a first reactor in the presence of hydrogen and in the presence or absence of a hydrogen-thermal cracking catalyst to be subjected to a hydrogen-thermal cracking reaction; (2) the reaction product in the first reactor is separated into light distillate, heavy wax oil and residual oil; (3) the residual oil and hydrogen enter a second reactor, and contact with the hydrogen-thermal cracking catalyst to be subjected to a hydrogen-thermal cracking reaction at a relatively low temperature; (4) the reaction product in the second reactor is separated into light distillate, heavy wax oil and residual oil, the separated heavy wax oil is returned to the first reactor, and the separated residual oil part is respectively returned to the two reactors for further reacting according to a proportion; and the reacting temperature in the second reactor is 5-50 DEG C lower than that in the first reactor. Compared with the prior art, the method has the advantages of remarkably improving the heavy oil conversion rate and light oil yield, and improving the light rate of heavy distillate.