51 results about "N alkanes" patented technology

A process for the production of sustainable aviation fuel (SAF) with low carbon intensity. The jet fuel is produced from the reaction of hydrogen from the electrolysis of water with captured carbon dioxide. The hydrogen and carbon dioxide are reacted to product a stream comprising carbon monoxide. Hydrogen and carbon monoxide are reacted to produce n-alkanes. Alkanes are hydroisomerized to produce sustainable aviation fuel with low carbon intensity.

The invention discloses an odorless temperature-controlled asphalt additive, odorless temperature-controlled asphalt and a preparation method of the odorless temperature-controlled asphalt. The odorless temperature control asphalt additive comprises the following components in parts by weight: 1-5 parts of odorless temperature control microcapsules; 1-5 parts of an auxiliary deodorant; 1-5 parts of a dispersant; the odor-removing temperature-control microcapsule comprises a composite shell material and a core material, the composite shell material comprises silicon dioxide / nano tourmaline / polydopamine, the core material comprises n-alkane with the phase change temperature of 40-60 DEG C, and a metal chelate and a smoke suppression compound containing active alpha-H are loaded on the surface of the composite shell material. The odorless temperature-controlled asphalt additive can efficiently and durably reduce the content of irritant gas in asphalt smoke, reduce the content of volatile organic compounds released by an asphalt pavement at high temperature, improve the high-temperature stability of asphalt and prolong the service time of the asphalt pavement, and provides a brand new idea for long-life and environment-friendly utilization of asphalt.

The invention discloses a method for complexing and separating n-alkanes in direct coal liquefaction oil, which comprises the following steps: 1) carrying out complexing reaction on the direct coal liquefaction oil and a complexing solution at 40-80 DEG C to obtain a complex suspension; 2) separating the complex suspension to obtain a complex and a filtrate; 3) demulsifying the filtrate at 20-60 DEG C, and separating out an oil phase to obtain an n-alkane removed oil product; wherein the complexing solution comprises a complexing agent, an activating agent and a solvent, the complexing agent is one or more of urea and thiourea, and the activating agent is low-carbon alcohol. The method effectively solves the problem that n-alkanes and isoalkanes in the direct coal liquefaction oil are difficult to separate.

This invention belongs to the field of petroleum processing technology, and specifically relates to a production apparatus and method for low-pour-point base oil for aviation hydraulic oil. The production apparatus and method for low-pour-point base oil for aviation hydraulic oil includes the following steps: Hydrorefining of the oil, where the feedstock oil undergoes hydrodesulfurization and dearomatization in a two-stage series process to produce hydrorefined oil with <1% aromatics and <1 mg / kg sulfur content; Fine fractionation of the oil, specifically: the hydrorefined oil is finely fractionated in a fractionation tower to obtain hydrorefined distillate oil at 230℃~280℃; Molecular sieve dewaxing, specifically: the 230℃~280℃ hydrorefined distillate oil is subjected to deep removal of n-alkanes using a 5A molecular sieve, lowering the oil's pour point to below -75℃, producing low-pour-point, low-aromatic aviation hydraulic oil base oil. This invention uses a combined process of "low-pressure hydrorefining-molecular sieve dewaxing" to produce a low-sulfur, low-aromatic, low-pour-point base oil with less than 1% aromatics. The production method has the advantages of low investment and ease of implementation.

The application discloses a petroleum drilling fluid aftereffect homing method, device, equipment and medium, and relates to the technical field of petroleum exploration. The method comprises the following steps: obtaining a target drilling fluid sample with bubble oil flower characteristics during drilling; analyzing and testing the target drilling fluid sample by means of logging technology to obtain n-alkane and isomeric alkane data corresponding to the target drilling fluid sample; determining chromatographic total hydrocarbon parameters and chromatographic component parameters according to the n-alkane and isomeric alkane data corresponding to the target drilling fluid sample; comparing and analyzing the chromatographic total hydrocarbon parameters and the chromatographic component parameters with total hydrocarbon parameters and component parameters of cuttings at different depths in a layer with oil and gas shows during drilling operation to determine the depth corresponding to the target drilling fluid sample and to homing the drilling fluid aftereffect with the bubble oil flower characteristics. In conclusion, the application can reduce the affected factors and make the homing error of the petroleum drilling fluid smaller.

A method for reducing the solid content in catalytic cracking slurry comprises: (1) mixing an auxiliary agent with raw oil and heating it to obtain a raw oil liquid, wherein the auxiliary agent is petroleum wax with a carbon number between C20 and C43 and a normal paraffin mass content of 35 to 60%; (2) mixing a diluent with the raw oil liquid in step (1), cooling to obtain a liquid-solid mixture, and performing solid-liquid separation to obtain a desolidified oil liquid and a wax paste, wherein the diluent is a C3-C6 fatty ketone and / or a C6-C8 aromatic hydrocarbon; (3) removing the diluent from the desolidified oil liquid to obtain a catalytic cracking slurry desolidified with solids, and removing the diluent from the wax paste to obtain the auxiliary agent containing solids. The method provided by the present invention has simple steps, and the solid removal rate of the catalytic cracking slurry is greater than 88%.

A method of producing hydrocarbons includes acidifying and extracting fatty acids from a feed solution that includes fatty acid salts using carbon dioxide (CO2); separating CO2 from the extracted fatty acids; recycling at least a portion of the separated CO2 to be used as the extractant; contacting at least a portion of the extracted fatty acids with a ketonization catalyst to produce ketones; contacting at least a portion of the ketones with a hydrodeoxygenation catalyst in the presence of hydrogen to produce n-paraffins. The n-paraffins may be subjected to hydrocarbon refining to produce hydrocarbons suitable for use as a sustainable aviation fuel, a sustainable diesel fuel, or a sustainable marine fuel.

The present application relates to a method for separating normal and isomeric alkanes in naphtha by inorganic membrane, which matches the membrane separation process with the actual working condition in industrial application to realize continuous production and directly obtain the purified product. The process first carries out hydrogenation pretreatment on full-range naphtha, then directly enters the membrane separation unit without pressure and temperature adjustment, and then obtains separated normal / isomeric alkane products, and finally enters the subsequent application production unit. The product rich in normal alkanes obtained on the permeation side after membrane separation can be used as high-quality raw material for the subsequent ethylene cracking section, and the product rich in isomeric alkanes obtained on the retentate side can be used as high-quality catalytic reforming or high-quality gasoline raw material. Coupling the membrane separation with the naphtha production process does not introduce the third component, is simple to operate, and has low energy consumption. The present application mainly solves the practical problems in the prior art, such as the difficulty in recovering the adsorbent, the large amount of desorbent, and the high energy consumption in the separation process when the adsorption method is used to separate normal and isomeric alkanes.

The application discloses a method for preparing liquid fuel by two-stage hydrogenation of soapstock, and belongs to the field of soapstock recycling and reuse. The method adopts a two-stage reactor in series, hydrogenation pyrolysis of soapstock is carried out in a first-stage reactor, and catalytic hydrogenation deoxygenation reaction of pyrolysis volatile products is carried out in a second-stage reactor, so that liquid fuel is finally obtained. The method has mild reaction conditions, a simple process, low hydrogen consumption, and improved stability of the catalyst, and can achieve excellent hydrogenation deoxygenation effect under low pressure, and the prepared liquid fuel is free of oxygen-containing products and is normal alkanes with carbon numbers of 5 to 19, and the yield can reach 86% at the highest. The method can realize high-value utilization of soapstock, and can relieve energy shortage and environmental pollution.

The present invention discloses a method for combined production of chemical raw materials by coking and hydrocracking. The method includes: the coking raw material enters the delayed coking reaction zone for thermal cracking reaction to obtain petroleum coke and gaseous effluent; the gaseous effluent is fractionated to obtain coker dry gas, coker light distillate oil and coker wax oil; wherein, the mass content of tricyclic aromatic hydrocarbons in the coker light distillate oil is not higher than 1.0%; the coker light distillate oil is mixed with hydrogen and undergoes a normal paraffin conversion reaction in the normal paraffin conversion reaction zone, and the mass content of C7+ normal paraffins in the reaction effluent is controlled to be 0.1% - 5.0%; in the presence of hydrogen, the normal paraffin conversion reaction effluent enters the hydrocracking reaction zone for hydrocracking reaction, and then the hydrocracking reaction effluent is separated and fractionated to obtain gas fraction, light naphtha, heavy naphtha and tail oil. This method uses coker light distillate oil as the raw material for hydrocracking to produce chemical raw materials, which can significantly improve the quality and yield of chemical raw materials.

The invention provides a method for precisely converting coal tar into high-cetane-number alkane through hydrogenation, which comprises the following steps: obtaining reaction data in a preliminary process condition range, if the hydrogenation depth exceeds a preset threshold value, adjusting a temperature control parameter to reduce the decyclization degree, and obtaining stable n-alkane generation efficiency through iterative calculation; according to the adjusted reaction path scheme, a hydrogenation process is operated in an actual reactor, a cetane number fluctuation range is extracted from real-time monitoring data, and whether process conditions and catalyst gradation adaptability meet target requirements or not is judged; if the fluctuation range of the cetane number exceeds a preset threshold value, analyzing the interaction influence of temperature control and pressure regulation through regression, and optimizing process conditions by adopting a gradient descent algorithm to obtain a final process parameter combination; long-term operation data of an accurate conversion result is obtained, the stability of catalyst grading and process conditions is analyzed through a machine learning algorithm, the dynamic adjustment requirement of a reaction path is judged, and a self-adaptive hydrogenation optimization model is obtained.

The invention discloses a method for preparing bio-based isoparaffins, and belongs to the technical field of organic chemical industry. The method is to convert bio-based lipid compounds into normal and isomeric mixed alkanes through hydrodeoxygenation and hydroisomerization reactions, and then obtain mixed alkanes with a carbon number of not less than 15 by normal pressure fractionation, and then separate normal and isoparaffins by molecular sieve adsorption and / or urea complexation. The obtained normal alkane is recycled back to the hydroisomerization unit for secondary hydroisomerization reaction, and the obtained high-purity isoparaffin is fractionated and / or rectified to obtain isoparaffin products of different fractions, which can be used as solvent oil, white oil, drilling fluid, aviation kerosene blending component, clean high cetane number diesel blending component, etc. The raw materials used in the present invention are renewable, and the prepared isoparaffin products are high in purity, high in yield, clean and environmentally friendly.

The present invention discloses a method for producing chemical raw materials by two-stage hydrocracking of wax oil. The method comprises: hydrocracking the wax oil raw material in the presence of hydrogen to first obtain a first hydrocracking product with a low polycyclic alkane content; then selectively cracking the normal paraffins in the first hydrocracking product to obtain a second hydrocracking product; separating and fractionating the second hydrocracking product to obtain gas, light naphtha, heavy naphtha, and tail oil; finally, mixing the tail oil with hydrogen and hydrocracking it to convert it into a third hydrocracking product containing monocyclic cyclic hydrocarbons; separating and fractionating the third hydrocracking product to obtain a gas fraction, light naphtha, and heavy naphtha; wherein the reaction pressure of the first hydrocracking reaction zone is 2.0 to 5.0 MPa higher than the reaction pressure of the third hydrocracking reaction zone. This method can significantly improve the yield and quality of chemical raw materials when using wax oil as a raw material for two-stage hydrocracking production of chemical raw materials.

The invention discloses a method for calculating coal rock maturity by simulating crude oil n-alkanes based on hydrocarbon generation heat. The method comprises the following steps: S1, collecting a rock core sample or a field outcrop sample; s2, performing a gold tube closed system hydrocarbon generation thermal simulation experiment on the sample, and collecting liquid hydrocarbon products generated at different temperature points; s3, performing gas chromatographic analysis on the liquid hydrocarbon product; s4, calculating the equivalent Ro of each temperature point, counting the peak area value of the n-alkanes at each temperature point, and selecting the n-alkanes with the carbon number of C6-C17 at each temperature point to calculate the sum of the peak areas; s5, fitting to obtain a function relation between the equivalent Ro and the sum of the peak areas of the n-alkanes; and S6, taking crude oil samples of the same hydrocarbon source rock source in the research area, measuring the n-alkane peak area of the crude oil, substituting peak area data into the function relation established in the step S5, and calculating to obtain the equivalent Ro of the crude oil samples. The method is suitable for quantitative calculation of crude oil maturity in all thermal evolution stages, and has important significance for oil-gas exploration.

The invention discloses a straight-run diesel hydrocracking method. After the straight-run diesel is hydrorefined, the hydrocracking reaction effluent is separated by a hydrocracking catalyst bed containing a ZSM‑5@β composite molecular sieve to obtain a naphtha fraction; the obtained naphtha component is passed through a normal isomerization adsorption separation device to obtain a component rich in normal alkanes and rich in isoalkanes, and the component rich in normal alkanes can be directly used as a raw material for steam cracking to produce ethylene, while the component rich in isoalkanes can be used as a high-quality National VI gasoline blending component. In the present invention, a ZSM‑5@β composite molecular sieve with strong paraffin cracking and isomerization capabilities is selected as an acidic center, which can effectively isomerize and crack the paraffins in diesel into the naphtha component to produce high-octane gasoline.

The present invention relates to a fuel composition comprising: (i) 60 to 94% by mass of a hydrocarbon mixture comprising: (a) 35 to 55% by mass of aromatic compounds; (b) 30 to 50% by mass of a mixture of n-paraffins and iso-paraffins containing at least 5 carbon atoms, with a ratio of the amount of iso-paraffins to the amount of n-paraffins greater than or equal to 3; and (c) 5 to 15% by mass of naphtenes; (ii) 5 to 36% by mass of ethanol; and (iii) 1 to 10% by mass of butane. This composition is useful for fuelling a spark ignition engine in motor vehicles intended for use by the general public or in competition.

An aviation fuel composition including an aromatic-based product generated by fluid catalytic cracking of a lipid feedstock in the presence of a fluid catalytic cracking, wherein the aromatic-based product comprises at least 50 vol. % aromatics, and a paraffinic-based product comprising normal paraffins and iso-paraffins in an amount of at least 85 vol. %. The aviation fuel composition meets the ASTM D1655-24b specification with the added requirements in Annex Al and / or the ASTM D7566-24d, Annexes A1-A8 specification requirements.

The present invention discloses a processing method for producing more chemical raw materials from crude oil. The method includes: the crude oil is subjected to atmospheric distillation to obtain the overhead oil of the atmospheric tower; wherein, the initial boiling point of the overhead oil of the atmospheric tower is 50°C to 80°C, and the final boiling point is 190°C to 240°C; in the presence of hydrogen, the overhead oil of the atmospheric tower enters the first hydrocracking reaction zone to selectively crack the n-alkanes in the overhead oil of the atmospheric tower to obtain the first hydrocracking product; wherein, the mass content of C7 + n-alkanes in the first hydrocracking product is controlled at 0.1% to 5.0%; in the presence of hydrogen, the first hydrocracking product enters the second hydrocracking reaction zone to obtain a second hydrocracking product containing monocyclic cyclic hydrocarbons; the second hydrocracking product is separated and fractionated to obtain a gas fraction, light naphtha, heavy naphtha and tail oil. When using the overhead oil of the atmospheric tower as the raw material to produce chemical raw materials, this method can significantly improve the yield and quality of chemical raw materials.

The present invention discloses a processing method for co-producing chemical raw materials by combining coking and hydrocracking. The method includes: the coking raw material enters the delayed coking reaction zone for thermal cracking reaction to obtain petroleum coke and a gaseous effluent; the gaseous effluent is fractionated to obtain coker dry gas and coker whole fraction oil; the initial boiling point of the coker whole fraction oil is 50°C to 80°C, and the final boiling point is 460°C to 520°C; in the presence of hydrogen, the coker whole fraction oil enters the first hydrocracking reaction zone to obtain a first hydrocracking product; the mass content of C7 + normal paraffins in the first hydrocracking product is controlled at 0.1% to 5.0%; the first hydrocracking product enters the second hydrocracking reaction zone, and the obtained second hydrocracking product is separated and fractionated to obtain a gas fraction, light naphtha, heavy naphtha and tail oil. This method uses heavy oils such as vacuum residue as raw materials, and can improve the quality and yield of chemical raw materials.

The present invention discloses a method for producing chemical raw materials by diesel hydrocracking. The method includes: (1) in the presence of hydrogen, a diesel raw material is mixed with hydrogen and enters a first hydrocracking reaction zone for first hydrocracking, and the mass content of C7 + n-alkanes in the first hydrocracking product is controlled to be 1 wt% to 3 wt%; (2) the reaction effluent from step (1) enters a second hydrocracking reaction zone to perform selective ring-opening cracking on polycyclic hydrocarbons to obtain a second hydrocracking product; the hydrogen-rich gas obtained after the gas-liquid separation of the second hydrocracking product through a separator is used as recycle hydrogen, and the liquid phase enters a fractionation system for fractionation to obtain gas, light naphtha, heavy naphtha and tail oil; (3) the tail oil is mixed with hydrogen and enters a third hydrocracking reaction zone to obtain a third hydrocracking product containing monocyclic hydrocarbons, and the third hydrocracking product enters a separation and fractionation system. This method can significantly improve the yield and quality of chemical raw materials.

The invention provides a method for screening thin oil in thin oil blending and viscosity reduction, and relates to the technical field of thick oil thin oil blending and viscosity reduction. The method comprises the following steps: obtaining gas concentration curves of each n-alkane sample, each quasi-component sample, a to-be-diluted thick oil sample and each thin oil sample; determining a standard curve according to the gas concentration curve and the average carbon number information of each n-alkane sample; according to the gas concentration curve of each sample, the standard curve determines the average carbon number information of each quasi-component sample, the average carbon number information of the thick oil sample to be doped with the thin oil and the average carbon number information of each thin oil sample; determining an average carbon number interval according to the average carbon number information of each quasi-component sample and a mixing experiment result; and determining a target thin oil sample according to the average carbon number interval, the average carbon number information of the heavy oil sample to be doped with the thin oil and the average carbon number information of each thin oil sample. According to the method, the technical effect of improving the thin oil screening accuracy is achieved.

The present invention discloses a processing method for producing chemical raw materials from vacuum residue. The method includes: mixing the vacuum residue raw material with hydrogen and entering a fluidized bed hydrocracking reaction zone for hydrothermal cracking reaction, and obtaining fluidized bed light distillate oil through separation and fractionation; wherein, the mass content of bicyclic aromatic hydrocarbons in the fluidized bed light distillate oil is 0.1% to 1.0%; in the presence of hydrogen, the fluidized bed light distillate oil enters a first hydrocracking reaction zone to obtain a first hydrocracking product; wherein, the mass content of C7+ normal paraffin in the first hydrocracking product is controlled to be 0.1% to 5.0%; in the presence of hydrogen, the first hydrocracking product enters a second hydrocracking reaction zone to obtain a second hydrocracking product; the second hydrocracking product is separated and fractionated to obtain a gas fraction, light naphtha, and heavy naphtha. This method uses vacuum residue as a raw material, which can greatly improve the quality and yield of chemical raw materials.

A process includes coprocessing a slurry hydroprocessing feed stream comprising a solid biomass feedstock and a liquid feedstock including one or more of fats, oils and greases in the presence of a slurry hydroprocessing catalyst and hydrogen in a slurry hydroprocessing zone and under slurry hydroprocessing conditions to produce a liquid hydroprocessing effluent having a first n-paraffin content and a first aromatic content, and coprocessing the liquid hydroprocessing effluent by subjecting the liquid hydroprocessing effluent to a hydrodeoxygenation catalyst and under hydrodeoxygenation reaction conditions to produce a hydrodeoxygenated liquid effluent, and subjecting the hydrodeoxygenated liquid effluent to a hydroisomerization catalyst and under hydroisomerization reaction conditions thereby producing a liquid hydrocarbon product having a second n-paraffin content less than the first n-paraffin content and a second aromatic content less than the first aromatic content.

The present invention belongs to the technical field of synthesis gas for preparing gasoline, and particularly relates to a SAPO-11 molecular sieve composite catalyst and its application in the direct conversion of synthesis gas to gasoline. The catalyst comprises component I and component II, and component I and component II are compounded together in a mechanical mixing manner. The active ingredient of component I is metal oxide, and component II is SAPO-11 molecular sieve. Using synthesis gas as the reaction raw material, the conversion reaction is carried out in a fixed bed or a moving bed. The reaction process has high product yield and selectivity. The selectivity of gasoline composed of C5-C 11 can reach 70-90%, the selectivity of aromatics in C5-C 11 is less than 30%, the ratio of isoparaffin to n-paraffin (iso / n) in C5-C 11 can reach 15-60, and at the same time, the selectivity of by-product methane is less than 3%, having good application prospects.

The invention relates to the technical field of petrochemical product analysis, in particular to a method for measuring n-alkane content and carbon number distribution of white oil based on gas chromatography-mass spectrometry, which comprises the following steps: carrying out gas chromatography-mass spectrometry detection on a white oil sample to obtain total ion flow and mass spectrometry data; determining retention time and peak area of n-alkanes with different carbon numbers in the total ion chromatogram according to the total ion current and the mass spectrum data; and according to the retention time and the peak area, obtaining the n-alkane content in the white oil sample, the proportion of each carbon number interval and the carbon number distribution. The separation effect is good, the test result is accurate and reliable, the content and carbon number distribution of the n-alkanes in the C12-C34 carbon number interval can be measured, a mass spectrum detector is used, the carbon number distribution interval defining accuracy is improved, a standard sample is not needed for comparison, the detection process is convenient and rapid, and application and popularization are facilitated.

The present invention discloses a method for hydrocracking wax oil. The method comprises: hydrocracking a wax oil feedstock in the presence of hydrogen to first obtain a first hydrocracking product with a low polycyclic alkane content; then selectively cracking the normal paraffins in the first hydrocracking product to obtain a second hydrocracking product; and finally converting the product into a third hydrocracking product containing monocyclic cyclic hydrocarbons. The third hydrocracking product is separated and fractionated to obtain a gas fraction, light naphtha, heavy naphtha, and tail oil. This method can significantly improve the yield and quality of chemical raw materials when hydrocracking wax oil is used as a feedstock to produce chemical raw materials.

The application discloses a kind of net taste temperature control asphalt additive, asphalt composition and preparation method thereof.Net taste temperature control asphalt additive of the application includes the following components by weight parts: auxiliary odor control agent, 1-5 parts;Dispersing agent, 1-10 parts;Odor control temperature microcapsule, 1-5 parts;The odor control temperature microcapsule includes composite shell material and core material, wherein the composite shell material includes inorganic base layer shell, barium titanate nanoparticles, polydopamine and cuprous oxide, the core material includes n-alkane with phase transition temperature of 40-60 DEG C, and the composite shell material surface is loaded with active smoke suppression compound.The net taste temperature control asphalt prepared by adding odor control temperature microcapsule into asphalt can efficiently and durably reduce the content of irritating gas in asphalt fume, reduce the content of volatile organic compounds released by asphalt pavement at high temperature, improve the high-temperature stability of asphalt, and prolong the service life of asphalt pavement by the temperature control effect of microcapsule and the odor control effect of active components on the surface of microcapsule.

The invention provides a complexation dewaxing method and system for separating n-alkanes in hydrocracking tail oil, and the complexation dewaxing method comprises the following steps: adding solid urea into liquid hydrocracking tail oil, and carrying out a complexation reaction to obtain a complexation mixture; and separating the complexing mixture to obtain a complex solid and a liquid-phase component. Mixing the complex solid with water, and carrying out a decomplexation reaction to obtain a first layered liquid; and separating the first layered liquid to obtain an n-alkane oil product and a first urea water product. The dewaxing is carried out by the method provided by the invention, and the n-alkane content of the n-alkane oil product is 20-50 wt% higher than the n-alkane content of the hydrocracking tail oil. According to the invention, the problem that the solvent is difficult to recover due to the addition of the active agent in the dewaxing process of the hydrocracking tail oil can be solved.

A method and apparatus for removing solids from catalytic cracking oil slurry, the method comprising: (1) mixing an auxiliary agent with raw oil and heating it to obtain a raw oil liquid, wherein the auxiliary agent is petroleum wax and / or synthetic wax, having a carbon number between C16 and C35 and a normal paraffin mass content of 70 to 85%; (2) mixing a diluent with the raw oil liquid in step (1), cooling it to obtain a liquid-solid mixture, and performing liquid-solid separation to obtain a desolidified oil liquid and a wax paste, wherein the diluent is a C3-C6 fatty ketone; (3) removing the diluent from the desolidified oil liquid to obtain a catalytic cracking oil slurry depleted of solids, and removing the diluent from the wax paste to obtain the auxiliary agent containing solids. The method provided by the present invention has simple steps, and the solids removal rate of the catalytic cracking oil slurry is greater than 86%.

The present invention discloses a method for producing chemical raw materials from vacuum residue. The method comprises: mixing the vacuum residue raw material with hydrogen and entering an ebullated bed hydrogenation reaction zone to carry out a hydrothermal cracking reaction, and separating and fractionating to obtain a gas fraction, a sideline oil, and a tail oil; wherein the mass content of aromatic hydrocarbons larger than three rings in the sideline oil is not higher than 1.0%; in the presence of hydrogen, the sideline oil enters a first hydrocracking reaction zone to obtain a first hydrocracking product; wherein, in the first hydrocracking product, C7 + The mass content of normal paraffins is controlled at 0.1% to 5.0%. The first hydrocracking product then enters a second hydrocracking reaction zone. The resulting second hydrocracking product is separated and fractionated to produce a gas fraction, light naphtha, heavy naphtha, and tail oil. This method, using vacuum residue as a feedstock, can significantly improve the yield and quality of chemical raw materials by combining ebullated-bed hydrogenation and hydrocracking to produce chemical raw materials.