55results about How to "Improve light oil yield" patented technology

The invention relates to the field of comprehensive utilization of oil shale, and provides a comprehensive utilization method of oil shale. Particularly, in the method, hydrogen production and oil hydrogenation processes of synthesis gas generated by oil shale dry distillation, dry distillation semicoke pre-charking, semicoke gasification after pre-charking, heavy oil recycle and gasification areorganically combined so as to obtain oil products from raw materials to the maximum extent, the oil products are hydrotreated to obtain high-quality clean oil products, the synthesis gas generated bygasification can be used as high-quality and cheap raw material for hydrogen production to provide a hydrogen source for oil product hydrogenation, and oil shale ash products obtained by cooling after gasification and complementary calcination are used as high-quality building materials. The invention provides a comprehensive utilization cleaner production process which can convert raw materials into high-quality products to the maximum extent and can fully utilize semicoke resources and rich production energy.

The invention relates to a preparation method of a catalytic cracking catalyst. According to the method, the NaY molecular sieve raw powder and halogen-containing gas are contact to perform gas phase ion exchange reaction; the sodium reduction and the ultra-stabilization of the NaY molecular sieve raw powder are completed in one step; the low-sodium high-silica-alumina-ratio molecular sieve is prepared. According to the method, different kinds of clay raw ores are compounded and are treated by high-concentration acid to obtain acid active composite clay; then, the low-sodium high-silica-alumina-ratio molecular sieve, the acid active composite clay, bonding agents, rare earth and decationized water are mixed and pulped; then, spraying granulation is performed; roasting and curing are performed; washing and drying are not needed; a finished product of the catalytic cracking catalyst is obtained. The catalytic cracking catalyst has the advantages that the olefin content in the gasoline can be obviously reduced; the light oil yield is improved; the preparation flow process of the catalyst is short; no ammonia and no nitrogen are discharged.

The invention aims at solving defects such as low light oil yield, high foam layer, and high coke yield of prior arts, and discloses a delayed coking method. The method is characterized in that: a mixed raw material is heated in a heating furnace; the heated hot material flow enters a primary hydrocyclone, such that a gas phase (1) and a mixed liquid phase (1) are obtained; the gas phase (1) is quenched and is delivered into a fractionation column; high-temperature steam is injected into the mixed liquid phase (1), and the mixture is delivered into a secondary hydrocyclone; the secondary hydrocyclone separates the mixed liquid phase (1) into a gas phase (2) and a mixed liquid phase (2). The gas phase (2) is delivered into a fractionation column; high-temperature steam is injected into the mixed liquid phase (2), and the mixture is delivered into a coke column; coke is discharged from the bottom of the coke column, and reaction oil gas is delivered into the fractionation column.

The present invention is industrial method of reusing waste plastics to produce gasoline and diesel oil. Waste plastics including polyethylene, polypropylene and polystyrene in certain proportion are mixed and heated to liquefy and crack inside one reactor with double-screw stirrer inside it and molten salt inside sandwiched layer as heat conducting medium; the produced material is viscosity reducing cracked and the cracked gas is condensated into liquid fed to rectifying tower; molten plastic liquid is pumped from the reactor into one solid-liquid separator with separating molten salt liquid to separate residue and dirt; clean molten plastic is returned to the reactor while the separated residue and dirt is exhausted via screw extruder in the bottom of the separator; and decompression distillation is performed to produce oil. The present invention can produce oil with high quality in low cost and high conversion rate while tackling white pollution.

The invention provides a method for improving the shale oil hydrorefining denitrification rate, and relates to a whole fraction shale oil hydro-denitrification process. The method aims at solving the technical problems that in the existing method for producing diesel oil through shale oil hydrorefining, the stability of a diesel oil product is low, and the operation running period of a hydrorefining catalyst is short. According to the method, a raw material pretreatment unit 1, a raw material pre-fractionation unit 2, a primary hydrorefining reaction unit 3, a secondary hydrorefining reaction unit 4 and a product fractionation unit 5 are used. When the method provided by the invention is used for processing shale oil, the light oil yield is high; the nitrogen content of the diesel oil product is low; the chromaticity and the stability conform to national V standard requirements; the goal of light oil product deep denitrification can be achieved; the service life of the hydrorefining catalyst is prolonged; the operation running period of the catalyst is improved. A main product of the method is hydrorefining diesel oil; byproducts are high-value LPG and hydrogenated naphtha; heavy shale oil and hydrogenation tail oil thrown out in the technical process can be further processed and used in a downstream device. The method provided by the invention belongs to the field of whole-fraction shale oil deep processing.

The invention discloses a preparation method for a metal deactivator applied to catalytic cracking and the metal deactivator prepared by using the same. The preparation method comprises the followingsteps: a, mixing antimony trioxide, hydroxycarboxylic acid, a rare-earth salt, a pH value conditioning agent and water and carrying out a reaction at a temperature of 20 to 90 DEG C for 30 to 60 min so as to obtain a first product; and b, mixing an oxidizing agent with the first product obtained in the step a, and carrying out a reaction in an enclosed container at a temperature of 100 to 150 DEGC for 1 to 2 h so as to obtain the metal deactivator applied to catalytic cracking. The preparation method for the metal deactivator applied to catalytic cracking has the advantages of simple process,short reaction time, low cost and reduction in energy consumption, and produces substantial economic benefits. The metal deactivator prepared by using the method has a good nickel and vanadium passivation function when applied to a catalytic cracking reaction and can obviously increasing the yield of light oil and reducing the proportions of coke and dry gas in a product.

The invention discloses the heavy and ungraded residual oil process method. The method comprises the following steps: hydrotreating the fixed bed and suspended bed, deasphalting and catalytic cracking the dissolvent, and graded treatmenting the heavy and ungraded residual oil raw material. The method comprises many characteristics, as follow: sufficiently utilizing the fixed bed and suspended bed by hydrotreating the two or more than two kinds of feeds respectively, improving the productivity of light oil; through adjusting the proportion of deasphalted oil in the feed of fixed bed hydrotreating, residual oil hydrogenation unit of fixed bed handling more residual oil, effectively decreasing the coke deposit rate on the hydrogenation catalyst, and extending the durability of catalyst; with the said technique, producing the more light end product.

The present invention relates to a cracking method of hydrocarbon oil, including contact of hydrocarbon oil with catalyst under the cracking condition. Said catalyst is a cracking catalyst containing laminar clay or mixture of said cracking catalyst containing laminar clay and existent cracking catalyst. The described cracking catalyst containing laminar clay is prepared by adopting the following steps: mixing expandable clay, modifying component, pseudo-thin hydrargillite and water, pulping for 0.1-10 hr. to obtain a slurry liquor, ageing for 0.1-10 hr. at 50-85 deg.C, drying, forming, washing with water, ageing, drying and roasting so as to obtain the invented catalyst. The described modifying component can be selected from hydroxyl polymer of silicon, aluminium, zirconium and titanium or substance containing the described hydroxyl polymer.

The invention provides an omnipotent bed hydrogenation technology. Raw materials comprise atmospheric pressure residual oil, vacuum residual oil, catalytic slurry oil, deoiled asphalt, coal tar or distillate oil, and can further comprise coal dust, firstly, the raw material oil and an oil soluble catalyst are mixed in a raw material/catalyst mixing system, the mixing temperature is 60-350 DEG C, and the mixing time is 20-200 minutes; the vulcanization process is completed in a reactor; the omnipotent bed is a cylindrical reactor excluding a fixed bed layer; the oil soluble catalyst is the combination of one or more of active components of Mo, Ni, Co, W, Fe. According to the omnipotent bed hydrogenation technology, firstly, the oil soluble catalyst and the raw material oil are mutually mixed (after an oil-coal joint hydrogenation technology, coal dust is added to prepare coal-oil slurry, and swelling is conducted), hydrogen is added, the temperature is raised, the pressure is raised, a reaction is conducted, separation is conducted, and fractional distillation is conducted. The omnipotent bed hydrogenation technology has the advantages of being high in raw material adaptability, high in light oil yield, less in atmospheric and solid waste and low in temperature and pressure.

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.

The invention provides a revolving bed coal catalytic pyrolysis method. The method comprises steps of raw coal pretreatment, catalyst preparation, powdered coal shaping with addition of the catalyst, catalyst briquette coal drying, and pyrolysis in a revolving bed thermal decomposition furnace, and the catalyst is one or some selected from vanadium titanium magnetite and Fe3O4. The method solves the problems that after powdered coal shaping with addition of the catalyst, the briquette coal is low in intensity, and is easy to pulverize during the pyrolysis process. The dust content in tar can be lowered, the tar yield is raised, and the tar quality is improved.

The present invention relates to a catalytic cracking oil slurry treatment method and a system thereof. The method comprises steps: enabling the catalytic cracking oil slurry and optional catalytic cracking recycle oil to enter a hydrotreating unit to contact with a catalyst in a hydrogenation reaction zone to react, and enabling a reaction effluent to enter a gas-liquid separation zone to be separated to obtain a hydrogen-rich gas and a liquid phase material flow, enabling the liquid-phase material flow and a catalytic cracking raw material to enter a riser reactor of a catalytic cracking unit together to be in contact with a catalytic cracking catalyst for reaction, and separating a reaction effluent to obtain catalytic cracking dry gas, liquefied gas, catalytic cracking gasoline, catalytic cracking diesel oil, catalytic cracking recycle oil and catalytic cracking oil slurry, and returning the catalytic cracking oil slurry to the hydrogenation reaction zone for reaction. According tothe invention, the operation period of the hydrotreating unit is prolonged, and the light oil yield of the catalytic cracking unit is improved.

The invention discloses a high-stability modified Y-type molecular sieve for high production of isomerized C4 and a preparation method of the high-stability modified Y-type molecular sieve. The CaO content of the modified Y-type molecular sieve is 0.3-4 wt%, the RE2O3 content is 2 to 7 wt%; the content of Na2O is 0.1 to 0.5 wt%; the total pore volume is 0.33 mL/g to 0.39 mL/g; the pore volume of the secondary pores of 2-100nm accounts for 10-25% of the total pore volume; the lattice constant is 2.440-2.455 nm, the content of non-framework aluminum accounts for not more than 20% of the total aluminum content, the lattice collapse temperature is not lower than 1050 DEG C, and the ratio of the amount of acid B to the amount of acid L measured by a pyridine adsorption infrared method at 200 DEG C is not lower than 2.30. The preparation method comprises the steps of ion exchange, modification treatment under certain temperature and water vapor conditions and reaction with silicon tetrachloride. The modified Y-type molecular sieve has higher heavy oil conversion activity, lower coke selectivity, higher gasoline yield and isomeric C4 yield, and higher isomeric hydrocarbon content in gasoline.

The invention relates to a settlement steam stripping method; a partition plate is arranged in a settler, and the settler and a steam stripping section at the lower part are divided into two spaces through the partition plate; a reaction oil-gas cyclone separator, a steam stripping outflow medium cyclone separator and a steam stripping outflow medium conveying pipe are arranged above the partitionplate in the settler; a steam stripping outflow medium enters the steam stripping outflow medium cyclone separator through the steam stripping outflow medium conveying pipe to be further separated, the steam stripping outflow medium is prevented from entering the settler, and coking of the settler is prevented.