A method and system for producing lubricating oil base stocks and industrial white oils

Abstract

The present disclosure relates to a method and system for producing lubricating oil base oil and industrial white oil, comprising: S1, subjecting residual oil to a solvent deasphalting unit for solvent deasphalting refining treatment to obtain deasphalted oil; S2, subjecting hydrogen, vacuum gas oil and the deasphalted oil to a hydrocracking unit to contact with a first hydrogenation catalyst to perform a first hydrogenation reaction to obtain a hydrogenation product oil, wherein the first hydrogenation catalyst comprises a hydrotreating catalyst, a hydrocracking catalyst and a hydrofining catalyst; S3, subjecting the hydrogenation product oil to a first separation unit for first separation treatment to obtain naphtha, aviation kerosene, diesel and tail oil; S4, subjecting the tail oil to a catalytic dewaxing reaction unit to contact with a second hydrogenation catalyst to perform a second hydrogenation reaction to obtain a hydrodewaxing oil, wherein the second hydrogenation catalyst comprises a hydroisomerization catalyst and a post-hydrofining catalyst; and S5, subjecting the hydrodewaxing oil to a second separation unit for second separation treatment to obtain the lubricating oil base oil and the industrial white oil.

Description

Technical Field

[0001] The disclosure relates to the field of producing base oils and industrial white oils, specifically, to a method and system for producing lubricating oil base oils and industrial white oils. Background Technology

[0002] Existing methods for producing Group III lubricating oil base oils with a viscosity index >120 generally use paraffinic crude oil, hydrocracking tail oil, etc., as feedstocks combined with hydrotreating. However, when using this method to process intermediate feedstocks to produce lubricating oil base oils with a viscosity index >120, deep conversion of the feedstock oil is generally required. Therefore, the following problems exist:

[0003] The stringent requirements for raw materials result in low lubricant yield and significant viscosity loss. Furthermore, the demanding reaction process leads to substantial viscosity loss, deterioration in oil color, and poor stability, resulting in high-viscosity oils of poor quality. Summary of the Invention

[0004] The purpose of this disclosure is to provide a method and system for producing lubricating oil base oil and industrial white oil, which can simultaneously produce high viscosity index base oil and high viscosity industrial white oil, thereby improving oil quality.

[0005] To achieve the above objectives, the first aspect of this disclosure provides a method for producing lubricating oil base oil and industrial white oil, comprising the following steps:

[0006] S1. The residual oil is fed into the solvent deasphalting unit for solvent deasphalting and refining treatment to obtain deasphalted oil;

[0007] S2. Hydrogen, vacuum wax oil and deasphalted oil are introduced into the hydrocracking unit and contacted with the first hydrocracking catalyst to carry out the first hydrocracking reaction and obtain hydrocracking product oil. The first hydrocracking catalyst includes a hydrotreatment catalyst, a hydrocracking catalyst and a hydrorefining catalyst.

[0008] S3. The hydrogenated oil is fed into the first separation unit for the first separation process to obtain naphtha, jet fuel, diesel oil and tail oil;

[0009] S4. The tail oil is brought into the catalytic dewaxing reaction unit and contacted with the second hydrogenation catalyst to carry out the second hydrogenation reaction, thereby obtaining hydrogenated dewaxed oil. The second hydrogenation catalyst includes a hydrogenation isomerization catalyst and a post-hydrogenation refining catalyst.

[0010] S5. The hydrodewaxed oil is introduced into the second separation unit for a second separation process to obtain lubricating oil base oil and industrial white oil.

[0011] Optionally, in step S1, the conditions for the solvent deasphalting and refining treatment include: in the extraction tower, the volume ratio of solvent to residual oil is (2-10):1, the temperature at the top of the extraction tower is 20-150℃, and the pressure is 2-6 MPa; preferably, the volume ratio of solvent to residual oil is (3-8):1, the temperature at the top of the extraction tower is 30-120℃, and the pressure is 3-5 MPa; optionally, the solvent is selected from one or more of hydrocarbons with 3-7 carbon atoms, condensate oil, light naphtha, and gasoline; preferably... The solvent includes propane, or the solvent includes propane and one or more selected from ethane, propylene, butane and pentane; more preferably, the propane content in the solvent is 80-100% by weight, preferably 90-100% by weight, more preferably 95-100% by weight; preferably, the solvent deasphalting and refining treatment results in the deasphalted oil having a carbon residue value of less than 10% by weight, preferably less than 6% by weight; optionally, the residue oil is selected from one or more selected from vacuum residue oil and atmospheric residue oil.

[0012] Optionally, along the flow direction of the mixed feedstock in the hydrocracking unit, the hydrotreatment catalyst, hydrocracking catalyst, and hydrorefining catalyst are arranged sequentially; step S2 includes: mixing the vacuum wax oil and the deasphalted oil and then introducing them into the hydrocracking unit, and first contacting the mixed feedstock with the hydrotreatment catalyst for a hydrotreatment reaction; then contacting the hydrocracking catalyst for a hydrocracking reaction; and then contacting the hydrorefining catalyst for a hydrorefining reaction to obtain the hydrotreated oil; preferably, along the flow direction of the mixed feedstock in the hydrocracking unit, the hydrotreatment catalyst, the hydrocracking catalyst, and the hydrorefining catalyst are arranged sequentially; step S2 includes: mixing the vacuum wax oil and the deasphalted oil and then introducing them into the hydrocracking unit, and first contacting the mixed feedstock with the hydrotreatment catalyst for a hydrotreatment reaction; then contacting the hydrocracking catalyst for a hydrorefining reaction to obtain the hydrotreated oil; preferably, along the flow direction of the mixed feedstock in the hydrocracking unit, the hydrotreatment catalyst, the hydrotreated catalyst, and the hydrorefining catalyst are arranged sequentially. A hydrogenation protectant is also provided upstream of the catalyst; the volume ratio of the hydrogenation protectant: hydrogenation treatment catalyst: hydrocracking catalyst: hydrorefining catalyst is (5-30):100:(60-250):(30-150); preferably (10-25):100:(80-200):(50-100); optionally, the volume ratio of the vacuum wax oil to the deasphalted oil is (3-20):1, preferably (5-10):1; preferably, the residual carbon value of the material after mixing the vacuum wax oil and the deasphalted oil is not greater than 2% by weight; preferably not greater than 1% by weight.

[0013] Optionally, in step S2, the processing conditions of the hydrocracking unit include: a hydrocracking reaction temperature of 300–450 °C, a hydrogen partial pressure of 8–25 MPa, and a volume hourly space velocity of 0.3–2.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (300–2500):1; preferably, the hydrogenation reaction temperature is 320–420°C, the hydrogen partial pressure is 10–20 MPa, and the volume hourly space velocity is 0.4–2.0 h⁻¹. -1The hydrogen-to-oil volume ratio is (400–2000):1; the hydrocracking reaction temperature is 320–450℃, the hydrogen partial pressure is 8–25 MPa, and the volume hourly space velocity is 0.3–2.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (300–2500):1; preferably, the hydrocracking reaction temperature is 340–420°C, the hydrogen partial pressure is 10–20 MPa, and the volume hourly space velocity is 0.4–2.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is (400–2000):1; the hydrorefining reaction temperature is 280–420℃, the hydrogen partial pressure is 8–25 MPa, and the volume hourly space velocity is 0.3–2.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (300–2500):1; preferably, the hydrogenation refining reaction temperature is 300–400°C, the hydrogen partial pressure is 10–20 MPa, and the volume hourly space velocity is 0.4–2.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (400-2000):1.

[0014] Optionally, in step S2, the hydrotreating catalyst comprises a first support, an active metal component, an optional first promoter, and an optional organic additive; wherein the first support is selected from one or more of alumina, silica, titanium dioxide, magnesium oxide, zirconium oxide, thorium oxide, beryllium oxide, natural zeolite, and clay; preferably selected from one or more of alumina and silica-alumina; the active metal component comprises a first metal component and a second metal component; the first active metal component is selected from one or more of nickel and cobalt; the second active metal component is selected from one or more of molybdenum and tungsten; the first promoter is selected from one or more of fluorine, boron, and phosphorus; the organic additive is selected from one or more of oxygen-containing organic compounds and nitrogen-containing organic compounds; preferably, the oxygen-containing organic compounds are selected from organic alcohols and organic acids. The nitrogen-containing organic compound is selected from one or more of the following: preferably, the nitrogen-containing organic compound is selected from one or more of the following: organic amines; more preferably, the oxygen-containing organic compound is selected from one or more of the following: ethylene glycol, glycerol, polyethylene glycol, diethylene glycol, butanediol, acetic acid, maleic acid, oxalic acid, aminotriacetic acid, 1,2-cyclohexanediaminetetraacetic acid, citric acid, tartaric acid, and malic acid; the nitrogen-containing organic compound is selected from one or more of the following: ethylenediamine, EDTA, and their ammonium salts; more preferably, the first support comprises γ-alumina; the active metal component comprises tungsten oxide and nickel oxide; the first auxiliary agent comprises fluorine; more preferably, based on the total weight of the hydrogenation catalyst, the nickel oxide content is 1-5% by weight, the tungsten oxide content is 12-35% by weight, the fluorine content is 1-9% by weight, and the balance is γ-alumina.

[0015] Optionally, in step S2, the hydrocracking catalyst includes a second support and one or more of Group VIII and Group VIB metals supported on the second support; preferably, the second support includes a Y-type molecular sieve and an amorphous composite oxide; the amorphous composite oxide is selected from one or more of silica, alumina, titanium dioxide, and zirconium oxide; more preferably, based on the total weight of the hydrocracking catalyst, the content of the Group VIII metal is 2-8% by weight, the content of the Group VIB metal is 12-33% by weight, the content of the Y-type molecular sieve is 1-30% by weight, and the content of the amorphous composite oxide is 50-80% by weight, wherein the Group VIII and Group VIB metals are in oxide form.

[0016] Optionally, in step S2, the hydrorefining catalyst includes a third support and a third active metal component supported on the third support; optionally, the third support is selected from one or more of alumina and silicon oxide; the third active metal component is selected from one or more of nickel, molybdenum and magnesium; preferably, based on the total weight of the hydrorefining catalyst, the third active metal, in oxide form, contains 0.5-2.6% magnesium oxide, 1.5-5.5% molybdenum oxide, 20-28% nickel oxide, and 64-78% of the third support.

[0017] Optionally, the saturated hydrocarbon content in the hydrogenated oil obtained in step S2 is greater than 80% by weight; preferably 90-100% by weight; more preferably 98-100% by weight.

[0018] Optionally, the tail oil obtained in step S3 has a sulfur content of less than 50 μg / g, a nitrogen content of less than 10 μg / g, a distillation range of more than 300°C, and a color greater than 16 Céperte. Preferably, the tail oil obtained in step S3 has a sulfur content of less than 20 μg / g, a nitrogen content of less than 5 μg / g, a distillation range of more than 320°C, and a color greater than 14 Céperte. More preferably, the tail oil obtained in step S3 has a sulfur content of less than 10 μg / g, a nitrogen content of less than 2 μg / g, a distillation range of more than 370°C, and a color greater than 12 Céperte.

[0019] Optionally, in step S4, the hydroisomerization catalyst and the post-hydrogenation refining catalyst are sequentially arranged along the material flow direction in the catalytic dewaxing reaction unit, so that after the tail oil enters the catalytic dewaxing reaction unit, it first contacts the hydroisomerization catalyst to carry out a hydroisomerization catalytic reaction; then it contacts the post-hydrogenation refining catalyst to carry out a post-hydrogenation refining reaction to obtain the hydrodewaxed oil; preferably, the content of the post-hydrogenation refining catalyst, based on the hydroisomerization catalyst, is 50-200% by volume, preferably 80-150% by volume.

[0020] Optionally, in step S4, the reaction conditions in the catalytic dewaxing reaction unit include: a hydroisomerization catalytic reaction temperature of 280–400°C, a pressure of 3–20 MPa, and a liquid hourly space velocity of 0.4–2.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is (300–1200):1; preferably, the hydroisomerization catalytic reaction temperature is 300–380°C, the pressure is 8–18 MPa, and the liquid hourly space velocity is 0.5–1.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (400–1000):1; the refining reaction temperature after hydrogenation is 150–300℃, the pressure is 3–20 MPa, and the liquid hourly space velocity is 0.4–2.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is (300–1200):1; preferably, the refining reaction temperature after hydrogenation is 180–250°C, the pressure is 8–18 MPa, and the liquid hourly space velocity is 0.5–1.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (400-1000):1.

[0021] Optionally, in step S4, the hydroisomerization catalyst comprises a mesoporous molecular sieve, an inorganic oxide, and a fourth active metal component; optionally, the mesoporous molecular sieve is a type with a short axis of... Major axis is The molecular sieve has a one-dimensional elliptical pore structure; preferably, the mesoporous molecular sieve is selected from one or more of ZSM-22, Nu-10, Theta-1, ISI-1, ZSM-23, SAPO-11, SAPO-31, and SAPO-41 molecular sieves; more preferably, the mesoporous molecular sieve is ZSM-22 molecular sieve; optionally, the fourth active metal component is selected from one or more of cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium, platinum, molybdenum, and tungsten; preferably platinum; optionally, the inorganic oxide is selected from one or more of alumina and silicon oxide; more preferably, based on the total weight of the hydroisomerization catalyst, the content of the mesoporous molecular sieve is 30-70% by weight, the content of the inorganic oxide is 30-70% by weight, and the content of the fourth active metal component in reduced state is 0.2-1% by weight.

[0022] Optionally, the post-hydrogenation refining catalyst comprises a silica-alumina support and a fifth active metal component supported on the silica-alumina support; preferably, based on the weight of the silica-alumina support, the silica-alumina support comprises 16-20% by weight of silicon (calculated as oxide) and 78-82% by weight of aluminum (calculated as oxide); optionally, the ratio of pyridine infrared β-acid to L-acid measured at 200°C on the silica-alumina support is 0.06-0.085; optionally, the fifth active metal component is selected from one or more of platinum and palladium; preferably, when the fifth active metal component is platinum and palladium, based on the total weight of the fifth active metal component (calculated as oxide), the content of reduced palladium is 0.1-5% by weight, more preferably 0.2-2% by weight; the content of reduced platinum is 0.1-5% by weight, more preferably 0.2-2% by weight.

[0023] A second aspect of this disclosure provides a system for producing lubricating oil base oil and industrial white oil. The system includes a solvent deasphalting unit, a hydrocracking unit, a first separation unit, a catalytic dewaxing reaction unit, and a separation unit arranged sequentially. The deasphalting unit is configured to perform solvent deasphalting refining treatment on residual oil to obtain deasphalted oil. The hydrocracking unit includes a first hydrocracking catalyst and is configured to contact hydrogen, vacuum wax oil, and the deasphalted oil from the deasphalting unit with the first hydrocracking catalyst to perform a first hydrocracking reaction to obtain hydrotreated oil. The first hydrocracking catalyst includes a hydrotreating catalyst and a hydrocracking catalyst. The first separation unit is configured to perform a first separation treatment on the hydrocracking product oil from the hydrocracking unit to obtain naphtha, jet fuel, diesel oil, and tail oil; the catalytic dewaxing reaction unit includes a second catalyst, and the catalytic dewaxing reaction unit is configured to contact the tail oil from the first separation unit with the second hydrocracking catalyst to carry out a second hydrocracking reaction to obtain hydrodewaxed oil; wherein the second hydrocracking catalyst includes a hydroisomerization catalyst and a post-hydrocracking refining catalyst; the second separation unit is configured to perform a second separation treatment on the hydrodewaxed oil from the catalytic dewaxing reaction unit to obtain lubricating oil base oil and industrial white oil.

[0024] Through the above technical solution, this disclosure provides a method and system for producing lubricating oil base oil and industrial white oil. The deasphalted oil obtained from deasphalting residual oil is introduced together with vacuum wax oil into a hydrocracking unit for reaction. This achieves the goal of producing both lubricating oil base oil and industrial white oil while improving resource utilization. Furthermore, the hydrocracking unit is equipped with a hydrorefining catalyst to enhance its aromatic saturation function, increasing the aromatic content of the hydrocracking product. Then, through the catalytic reaction of the hydroisomerization catalyst and the post-hydrocracking refining catalyst in the catalytic dewaxing reaction unit, the goal of producing high viscosity index base oil and high viscosity industrial white oil is achieved, thereby improving oil quality.

[0025] Other features and advantages of this disclosure will be described in detail in the following detailed description section. Attached Figure Description

[0026] The accompanying drawings are provided to further illustrate the present disclosure and form part of the specification. They are used together with the following detailed description to explain the present disclosure, but do not constitute a limitation thereof. In the drawings:

[0027] Figure 1 This is an exemplary flowchart of a method and system for producing lubricating oil base oil and industrial white oil provided in this disclosure. Detailed Implementation

[0028] The following provides a detailed description of specific embodiments of this disclosure. It should be understood that the specific embodiments described herein are for illustrative and explanatory purposes only and are not intended to limit this disclosure.

[0029] This disclosure provides a method for producing lubricating oil base oil and industrial white oil, such as Figure 1 As shown, it includes the following steps:

[0030] S1. The residual oil is fed into the solvent deasphalting unit for solvent deasphalting and refining treatment to obtain deasphalted oil;

[0031] S2. Hydrogen, vacuum wax oil and deasphalted oil are introduced into the hydrocracking unit and contacted with the first hydrocracking catalyst to carry out the first hydrocracking reaction and obtain hydrocracking product oil. The first hydrocracking catalyst includes a hydrotreatment catalyst, a hydrocracking catalyst and a hydrorefining catalyst.

[0032] S3. The hydrogenated oil is fed into the first separation unit for the first separation process to obtain naphtha, jet fuel, diesel oil and tail oil;

[0033] S4. The tail oil is brought into the catalytic dewaxing reaction unit and contacted with the second hydrogenation catalyst to carry out the second hydrogenation reaction, thereby obtaining hydrogenated dewaxed oil. The second hydrogenation catalyst includes a hydrogenation isomerization catalyst and a post-hydrogenation refining catalyst.

[0034] S5. The hydrodewaxed oil is introduced into the second separation unit for a second separation process to obtain lubricating oil base oil and industrial white oil.

[0035] This disclosure provides a method for producing lubricating oil base oil and industrial white oil. The deasphalted oil obtained from deasphalting residual oil is introduced into a hydrocracking unit for reaction with vacuum wax oil. This method can improve resource utilization while simultaneously producing lubricating oil base oil and industrial white oil. Furthermore, the hydrocracking unit is equipped with a hydrorefining catalyst to enhance its aromatic saturation function, increasing the aromatic content of the hydrocracking product. Then, through catalytic reactions with a hydroisomerization catalyst and a post-hydrorefining catalyst in a catalytic dewaxing reaction unit, the method achieves the production of high viscosity index base oil and high viscosity industrial white oil, thereby improving oil quality.

[0036] In one specific embodiment, the residue oil is selected from one or more of vacuum residue oil and atmospheric residue oil; preferably, it is vacuum residue oil.

[0037] In this disclosure, the method and conditions for solvent deasphalting and refining can be conventional methods and conditions, and can include three steps: mixing, extraction and sedimentation separation. For example, it can be carried out in an extraction and sedimentation system consisting of an extraction tower and a sedimentation tower: first, the residual oil is mixed with the solvent and then sent to the extraction tower for full extraction, and then sedimentation separation is carried out in the sedimentation tower to complete the solvent deasphalting process.

[0038] In one embodiment, the conditions for the solvent deasphalting and refining treatment in step S1 include:

[0039] In the extraction tower, the volume ratio of solvent to residue oil is (2-10):1, the top temperature of the extraction tower is 20-150℃, and the pressure is 2-6MPa; preferably, the volume ratio of solvent to residue oil is (3-8):1, the top temperature of the extraction tower is 30-120℃, and the pressure is 3-5MPa.

[0040] In one embodiment, the solvent is selected from one or more of hydrocarbons with 3 to 7 carbon atoms, condensate oil, light naphtha, and gasoline; preferably, the solvent includes propane, or the solvent includes propane and one or more of ethane, propylene, butane, and pentane; more preferably, the propane content in the solvent is 80 to 100% by weight, preferably 90 to 100% by weight, more preferably 95 to 100% by weight; and more preferably 98 to 100% by weight.

[0041] In one specific embodiment, the solvent deasphalting and refining treatment results in the deasphalted oil having a residual carbon value of less than 10% by weight, preferably less than 6% by weight; a color value of no greater than 8; a content of n-heptane-insoluble matter of no greater than 200 ppm; and a drying point of the light deasphalted oil of no greater than 700°C. In this disclosure, color refers to the color value measured using GB / T 6540.

[0042] In one embodiment, the hydrotreatment catalyst, hydrocracking catalyst, and hydrorefining catalyst are sequentially arranged along the flow direction of the mixed feedstock in the hydrocracking unit; step S2 includes:

[0043] The vacuum wax oil and the deasphalted oil are mixed and then introduced into the hydrocracking unit. The mixed feedstock is first contacted with the hydrotreatment catalyst for a hydrotreatment reaction; then it is contacted with the hydrocracking catalyst for a hydrocracking reaction; and finally it is contacted with the hydrorefining catalyst for a hydrorefining reaction to obtain the hydrotreated oil.

[0044] In a preferred embodiment, the hydrocracking unit is further provided with a hydroprotective agent; along the material flow direction in the hydrocracking unit, the hydroprotective agent is positioned upstream of the hydrotreatment catalyst, so that the vacuum wax oil and the deasphalted oil mixture first come into contact with the hydroprotective agent in the hydrocracking unit for a hydroprotective reaction, and then sequentially come into contact with the hydrotreatment catalyst, the hydrocracking catalyst, and the hydrorefining catalyst for a reaction.

[0045] In one embodiment, the volume ratio of the hydrogenation protectant: hydrogenation treatment catalyst: hydrocracking catalyst: hydrorefining catalyst is ((5-30): 100: (60-250): (30-150).

[0046] In a preferred embodiment, the volume ratio of the hydrotreating protectant: hydrotreatment catalyst: hydrocracking catalyst: hydrorefining catalyst is (10-25):100:(80-200):(50-100). Using the above four catalysts according to this embodiment can achieve better hydrocracking results in the hydrocracking unit.

[0047] In one embodiment, the volume ratio of the depressurized wax oil to the deasphalted oil is (3-20):1, preferably (5-10):1;

[0048] Preferably, the residual carbon value of the mixture of the vacuum wax oil and the deasphalted oil is not greater than 2% by weight; more preferably, it is not greater than 1% by weight.

[0049] In this disclosure, the hydrocracking unit reaction in step S2 is primarily used to remove gum, sulfur, and nitrogen compounds from the feedstock, as well as the aromatic saturation and ring-opening reactions, so that they are converted into useful lubricating oil components. Therefore, provided that this objective is sufficient, the method and conditions can be conventional methods and conditions.

[0050] In one specific embodiment, the processing conditions of the hydrocracking unit in step S2 include:

[0051] The hydrogenation reaction was carried out at temperatures of 300–450 °C, hydrogen partial pressures of 8–25 MPa, and volume hourly space velocities of 0.3–2.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (300-2500):1;

[0052] The hydrocracking reaction is carried out at temperatures of 320–450 °C, hydrogen partial pressures of 8–25 MPa, and volume hourly space velocities of 0.3–2.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (300-2500):1;

[0053] The hydrogenation purification reaction is carried out at temperatures of 280–420 °C, hydrogen partial pressures of 8–25 MPa, and volume hourly space velocities of 0.3–2.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (300-2500):1;

[0054] Optionally, the hydrogenation protection reaction is carried out at a temperature of 300–430 °C, a hydrogen partial pressure of 8–25 MPa, and a volume hourly space velocity of 2.5–15 h⁻¹. -1 Hydrogen-to-oil volume ratio (300-2500): 1.

[0055] This disclosure adds a hydrorefining reaction after the hydrotreatment and hydrocracking reactions, which can further improve the degree of hydrosaturation and increase the viscosity and quality of the final lubricating oil base oil and industrial white oil. In this disclosure, the reaction temperature refers to the average reaction temperature in each catalytic reaction.

[0056] In a preferred embodiment, the hydrogenation reaction is carried out at a temperature of 320–420°C, a hydrogen partial pressure of 10–20 MPa, and a volume hourly space velocity of 0.4–2.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is (400-2000):1;

[0057] The hydrocracking reaction is carried out at temperatures of 340–420 °C, hydrogen partial pressures of 10–20 MPa, and volume hourly space velocities of 0.4–2.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is (400-2000):1;

[0058] Preferably, the hydrogenation refining reaction is carried out at a temperature of 300–400°C, a hydrogen partial pressure of 10–20 MPa, and a volume hourly space velocity of 0.4–2.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (400-2000):1;

[0059] Optionally, the hydrogenation protection reaction is carried out at a temperature of 320–420 °C, a hydrogen partial pressure of 10–20 MPa, and a volume hourly space velocity of 4–12 h⁻¹. -1 The hydrogen-to-oil volume ratio is (400-2000):1. Performing the hydrotreating process in step S2 according to this embodiment can further improve the hydrotreating effect and obtain oils of better quality.

[0060] In one embodiment, the hydrotreating catalyst comprises a first support, an active metal component, an optional first auxiliary agent, and an optional organic additive.

[0061] The first carrier comprises a heat-resistant inorganic oxide carrier, and the first carrier is selected from one or more of alumina, silicon oxide, titanium oxide, magnesium oxide, zirconium oxide, thorium oxide, beryllium oxide, natural zeolite, and clay; for example, the first carrier may be selected from one or more of alumina, silicon oxide, titanium oxide, magnesium oxide, silicon oxide-alumina, alumina-magnesium oxide, silicon oxide-magnesium oxide, silicon oxide-zirconium oxide, silicon oxide-thorium oxide, silicon oxide-beryllium oxide, silicon oxide-titanium oxide, silicon oxide-zirconium oxide, titanium oxide-zirconium oxide, silicon oxide-alumina-thorium oxide, silicon oxide-alumina-titanium oxide, silicon oxide-alumina-magnesium oxide, silicon oxide-alumina-zirconium oxide, natural zeolite, and clay; preferably, it is selected from one or more of alumina and silicon oxide-alumina (composite carrier);

[0062] The active metal component includes a first metal component and a second metal component; the first active metal component is selected from one or more of nickel and cobalt; the second active metal component is selected from one or more of molybdenum and tungsten.

[0063] The first auxiliary agent is selected from one or more of fluorine, boron and phosphorus;

[0064] The organic additive is selected from one or more of oxygen-containing organic compounds and nitrogen-containing organic compounds; preferably, the oxygen-containing organic compound is selected from one or more of organic alcohols and organic acids; preferably, the nitrogen-containing organic compound is selected from one or more of organic amines; more preferably, the oxygen-containing organic compound is selected from one or more of ethylene glycol, glycerol, polyethylene glycol, diethylene glycol, butanediol, acetic acid, maleic acid, oxalic acid, aminotriacetic acid, 1,2-cyclohexanediaminetetraacetic acid, citric acid, tartaric acid, and malic acid; the nitrogen-containing organic compound is selected from one or more of ethylenediamine, EDTA (ethylenediaminetetraacetic acid), and their ammonium salts.

[0065] In a preferred embodiment, based on the total weight of the hydrotreating catalyst, the content of the first active metal, calculated as oxide, is 1-5% by weight; the content of the second active metal, calculated as oxide, is 12-35% by weight; and the content of the first auxiliary agent, calculated as element, is 0-9% by weight. Optionally, the molar ratio of the organic matter to all active metal components, calculated as oxide, is 0-2:1.

[0066] In one specific embodiment, the first carrier comprises γ-alumina, the active metal component comprises tungsten oxide and nickel oxide, and the first additive comprises fluorine; preferably, based on the total weight of the hydrogenation catalyst, the nickel oxide content is 1-5% by weight, the tungsten oxide content is 12-35% by weight, the fluorine content is 1-9% by weight, and the balance is γ-alumina.

[0067] The catalysts used in this disclosure may be selected from one or more of the prior art catalysts capable of achieving this function. They may be commercially available or prepared using any existing method.

[0068] In one specific embodiment, the hydrorefining catalyst is designated as I, and the hydrorefining catalyst I can be selected from one or more of the following catalysts.

[0069] The catalyst disclosed in CN85104438A is composed of γ-Al2O3-supported tungsten and nickel oxides and fluorine as an auxiliary agent. Its composition (by weight) includes: nickel oxide of 1-5% by weight, tungsten oxide of 12-35% by weight, and fluorine of 1-9% by weight.

[0070] CN1853780A discloses a fluorine- and phosphorus-containing hydrogenation catalyst supported on silica-alumina. The calcined catalyst has the following composition: 1-10 wt% nickel oxide, a sum of molybdenum oxide and tungsten oxide greater than 10-50 wt%, 1-10 wt% fluorine, 0.5-8 wt% phosphorus oxide, and the balance being silica-alumina. The catalyst is prepared by a method including introducing fluorine, phosphorus, molybdenum, nickel, and tungsten into the silica-alumina support. The amounts of each component are such that the calcined catalyst composition is: 1-10 wt% nickel oxide, a sum of molybdenum oxide and tungsten oxide greater than 10-50 wt%, 1-10 wt% fluorine, 0.5-8 wt% phosphorus oxide, and the balance being silica-alumina.

[0071] CN1872959A discloses a fluorinated hydrogenation catalyst supported on alumina. The calcined catalyst has the following composition: 1-10 wt% nickel oxide, 10-50 wt% molybdenum oxide and tungsten oxide, 1-10 wt% fluorine, and the remainder being alumina. The preparation method of this catalyst includes introducing fluorine, molybdenum, nickel, and tungsten into an alumina support, wherein the amounts of each component are such that the calcined catalyst composition is: 1-10 wt% nickel oxide, 10-50 wt% molybdenum oxide and tungsten oxide, 1-10 wt% fluorine, and the balance being alumina.

[0072] The preparation method of the above-mentioned hydrorefining catalyst I is described in more detail in the aforementioned patent documents, which are also cited here as part of this disclosure.

[0073] In one embodiment, in step S2, the hydrocracking catalyst includes a second support and one or more of group VIII metals and group VIB metals supported on the second support.

[0074] Preferably, the second carrier comprises a Y-type molecular sieve and an amorphous composite oxide; more preferably, the amorphous composite oxide is selected from one or more of silicon oxide, aluminum oxide, titanium oxide and zirconium oxide.

[0075] In a preferred embodiment, based on the total weight of the hydrocracking catalyst, the content of Group VIII metals is 2-8% by weight, the content of Group VIB metals is 12-33% by weight, the content of Y-type molecular sieve is 1-30% by weight, and the content of amorphous composite oxides is 50-80% by weight, wherein the Group VIII metals and Group VIB metals are in oxide form.

[0076] The hydrocracking catalyst II used in this disclosure can be selected from one or more of the prior art catalysts capable of performing this function. They can be commercially available or prepared using any existing method.

[0077] In one specific embodiment, the most probable pore size of the second support in the hydrocracking catalyst described in step S2 is 3–20 nm, and the pore size concentration of the second support is 15–42. The most probable pore size is determined using the BET method. The pore size concentration refers to the ratio of the peak height to the full width at half maximum (FWHM) of the peak in the dV / dr distribution curve as a function of pore size, determined by the BET method. dV / dr represents the derivative of the specific pore volume with respect to the pore size. Preferably, the most probable pore size of the second support is 5–15 nm, and the pore size concentration of the support is 18–40.

[0078] In one specific embodiment, the Y-type molecular sieve in the hydrocracking catalyst is obtained through modification treatment. The modification treatment may specifically include rare earth exchange treatment, dealumination treatment, etc. The dealumination treatment includes thermal or hydrothermal dealumination, chemical dealumination, or a combination of both. The conditions for hydrothermal dealumination include calcining the NHY molecular sieve in the presence of steam, thereby extracting framework aluminum into non-framework aluminum, increasing the framework silicon-to-aluminum ratio, and decreasing the cell constant and ion exchange capacity. Changing the treatment temperature, time, and steam partial pressure can adjust the degree of dealumination and the size of the cell constant. The chemical dealumination methods include: EDTA complexation dealumination, SiCl gas-phase isomorphic substitution dealumination, (NH)SiF liquid-phase isomorphic substitution dealumination, and oxalic acid liquid-phase complexation dealumination. One method combines hydrothermal and chemical dealuminization. Specific conditions include: first, hydrothermal dealuminization, followed by chemical treatment to remove non-framework aluminum; acid, alkali solutions, salts (such as KF), complexing agents (such as EDTA) can be used. While using weak acid for dealuminization, the remaining Na in the molecular sieve system is also removed.

[0079] In one specific embodiment, the second support for the hydrocracking catalyst is prepared by the following method: mixing an amorphous composite oxide precursor, a Y-type molecular sieve, a peptide, and water to obtain a raw material mixture; feeding the raw material mixture into an extruder, and extruding it after kneading to obtain a molded body; calcining the molded body to obtain the second support, wherein the temperature of the molded body at the outlet of the extruder is 40–150°C. The amount of raw materials added during the preparation of the second support can be adjusted according to the target composition of the second support; the preparation process conditions can also adopt conventional process conditions in the art.

[0080] In a preferred embodiment, in step S2, the hydrorefining catalyst includes a third support and a third active metal component supported on the third support; the third support is selected from one or more of alumina and silica; the third active metal component is selected from one or more of nickel, molybdenum, and magnesium. In this disclosure, the introduction of three active metal components—nickel, molybdenum, and magnesium—into the hydrorefining catalyst, especially the introduction of magnesium, is beneficial in preventing cracking reactions under the high-temperature conditions of post-refining treatment, thereby improving the quality of the tail oil.

[0081] In a preferred embodiment, based on the total weight of the hydrorefining catalyst, the third active metal, in oxide form, comprises 0.5–2.6 wt% magnesium oxide, 1.5–5.5 wt% molybdenum oxide, 20–28 wt% nickel oxide, and 64–78 wt% third support.

[0082] In this disclosure, the hydrorefining catalyst is referred to as III. The hydrorefining catalyst III can be selected from one or more catalysts in the prior art that can achieve this function. They can be commercially available or prepared using any existing method.

[0083] In this disclosure, the method and conditions for step S3, which involves entering the first separation unit for the first separation process, are conventional methods and conditions. For example, separation is performed using distillation, a method known in the art, which typically includes one or more flash distillation, atmospheric distillation, and vacuum distillation units to achieve the desired separation. The apparatus used for the first separation process also has a conventional structure in the art.

[0084] In one specific embodiment, the tail oil obtained in step S3 has a sulfur content of less than 50 μg / g, a nitrogen content of less than 10 μg / g, a distillation range of more than 300°C, and a color greater than 16 Cépôt.

[0085] In a preferred embodiment, the sulfur content of the separated tail oil is less than 20 μg / g, the nitrogen content is less than 5 μg / g, the distillation range is above 320°C, and the color is greater than 14 Cépôt.

[0086] In a more preferred embodiment, the separated tail oil has a sulfur content of less than 10 μg / g, a nitrogen content of less than 2 μg / g, a distillation range of 370°C or higher, and a color greater than 12 Cépôt. In this disclosure, the color of the tail oil is determined by the Cépôt method (GB / 3555).

[0087] The catalytic dewaxing reaction unit in step S4 of this disclosure is intended for the hydrogenation conversion of large linear hydrocarbon molecules. The catalyst used is selected from one or more of the catalytic dewaxing catalysts and isomerization dewaxing catalysts well known in the art.

[0088] In one specific embodiment, in step S4, the hydroisomerization catalyst and the post-hydrogenation refining catalyst are sequentially arranged along the material flow direction in the catalytic dewaxing reaction unit, so that after the tail oil enters the catalytic dewaxing reaction unit, it first contacts the hydroisomerization catalyst to carry out a hydroisomerization catalytic reaction, and then contacts the post-hydrogenation refining catalyst to carry out a hydrorefining reaction, thereby obtaining the hydrodewaxed oil.

[0089] In a preferred embodiment, the content of the hydrogenated purification catalyst, based on the hydrogenation isomerization catalyst, is 50-200% by volume, preferably 80-150% by volume.

[0090] In one embodiment, in step S4, the reaction conditions in the catalytic dewaxing reaction unit include: a hydroisomerization catalytic reaction temperature of 280–400°C, a pressure of 3–20 MPa, and a liquid hourly space velocity of 0.4–2.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is (300–1200):1; the refining reaction temperature after hydrogenation is 150–300℃, the pressure is 3–20 MPa, and the liquid hourly space velocity is 0.4–2.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is (300-1200):1.

[0091] In one embodiment, in step S4, the reaction conditions in the catalytic dewaxing reaction unit include: a hydroisomerization catalytic reaction temperature of 300–380°C, a pressure of 8–18 MPa, and a liquid hourly space velocity of 0.5–1.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (400–1000):1; the refining reaction temperature after hydrogenation is 180–250℃, the pressure is 8–18 MPa, and the liquid hourly space velocity is 0.5–1.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (400-1000):1.

[0092] In one specific embodiment, the hydroisomerization catalyst comprises a mesoporous molecular sieve, an inorganic oxide, and a fourth active metal component;

[0093] Preferably, the mesoporous molecular sieve is a type with a short axis of Major axis is The molecular sieve has a one-dimensional elliptical pore structure; preferably, the mesoporous molecular sieve is selected from one or more of ZSM-22, Nu-10, Theta-1, ISI-1, ZSM-23, SAPO-11, SAPO-31, and SAPO-41 molecular sieves; more preferably, the mesoporous molecular sieve is ZSM-22 molecular sieve.

[0094] Preferably, the fourth active metal component is selected from one or more of cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium, platinum, molybdenum, and tungsten; more preferably, platinum;

[0095] Preferably, the inorganic oxide is selected from one or more of alumina and silicon oxide.

[0096] In a preferred embodiment, based on the total weight of the hydroisomerization catalyst, the content of the mesoporous molecular sieve is 30-70% by weight, the content of the inorganic oxide is 30-70% by weight, and the content of the fourth active metal component in reduced state is 0.2-1% by weight.

[0097] The hydroisomerization catalyst described in this disclosure is V, which can be selected from one or more catalysts in the prior art that can achieve this function. They can be commercially available or prepared using any existing method.

[0098] In one specific embodiment, the hydroisomerization catalyst V is selected from one or more of the following catalysts.

[0099] CN1448484A discloses a zeolite-containing catalytic dewaxing catalyst. The catalyst contains a zeolite-containing support and a hydrogenation metal component. The zeolite is a high-silica zeolite with a rare earth five-membered ring structure. The molar ratio of silicon oxide to aluminum oxide in the zeolite is 20 to 100. Based on the total amount of zeolite, the content of rare earth oxides is 0.1 to 2.5% by weight, and the content of sodium oxide is 0.1 to 1.5% by weight.

[0100] CN1382526A discloses a catalyst containing a silicon-phosphorus-aluminum molecular sieve, wherein the silicon-phosphorus-aluminum molecular sieve has a crystallinity of at least 70%, and the preparation method of the silicon-phosphorus-aluminum molecular sieve includes drying and calcining a mixture of a silicon-phosphorus-aluminum molecular sieve containing an organic template agent and an aqueous solution of an acid, wherein the weight ratio of the acid to the molecular sieve is 0.001 to 1.

[0101] CN106466624A discloses a method for preparing a hydrodewaxing catalyst, comprising the following steps: a) impregnating a molecular sieve-inorganic oxide support with a solution containing a hydrogenation active metal salt, followed by drying, calcination, and reduction to obtain a supported catalyst; wherein the molecular sieve is a molecular sieve with a one-dimensional elliptical pore structure, the minor axis of the one-dimensional elliptical pore structure being 4.2–5.4 Å, and the major axis of the one-dimensional elliptical pore structure being 5.4–7.0 Å; b) impregnating the supported catalyst obtained in step a) with water and drying to obtain a hydrodewaxing catalyst; wherein the weight loss of the hydrodewaxing catalyst after calcination at 450°C for 4 hours is 0.2–5.0 wt%.

[0102] CN101722037A discloses a catalyst for hydrodewaxing of lubricating oil distillate. The catalyst contains molecular sieves and hydrogenation metal components. The content of the hydrogenation metal components, based on the metal content and catalyst, is 0.1-5% by weight. The molecular sieve is a mixture of TON-type molecular sieves and ZSM-5. Based on the total amount of molecular sieves, the content of ZSM-5 molecular sieves in the mixture is 0.1-4% by weight.

[0103] More detailed methods for preparing the aforementioned catalysts are described in the aforementioned patent documents, which are also incorporated herein by reference as part of this disclosure.

[0104] In step S4 of this disclosure, the post-hydrogenation refining catalyst aims to saturate aromatic hydrocarbons with hydrogen. The catalyst used is selected from one or more well-known hydrorefining catalysts in the art.

[0105] In one embodiment, the post-hydrogenation refining catalyst comprises a silica-alumina support and a fifth active metal component supported on the silica-alumina support;

[0106] Preferably, based on the weight of the silicon-aluminum support, the silicon-aluminum support comprises 16-20% by weight of silicon (calculated as oxide) and 78-82% by weight of aluminum (calculated as oxide); optionally, the ratio of pyridine infrared β-acid to L-acid measured at 200°C on the silicon-aluminum support is 0.06-0.085.

[0107] Optionally, the fifth active metal component is selected from one or more of platinum and palladium;

[0108] Preferably, when the fifth active metal component is platinum and palladium, the content of reduced palladium is 0.1-5% by weight, more preferably 0.2-2% by weight, and the content of reduced platinum is 0.1-5% by weight, more preferably 0.2-2% by weight, based on the total weight of the fifth active metal component calculated as oxides.

[0109] In one specific embodiment, the post-hydrogenation refining catalyst is VI, and the post-hydrogenation refining catalyst VI is selected from one or more of the following catalysts.

[0110] CN103041832A discloses an aromatic hydrocarbon hydrogenation saturated catalyst comprising a silica-alumina support and a hydrogenation-active metal component supported on the silica-alumina support. The silica-alumina support, measured at 200°C, has a pyridine infrared ratio of β-acid to L-acid of 0.13–0.15. Based on the weight of the silica-alumina support, the silica-alumina support contains 42–46 wt% silicon (calculated as oxides), 52–56 wt% aluminum (calculated as oxides), 0–0.2 wt% alkali metal (calculated as oxides), and 0.5–4 wt% fluorine (calculated as elements).

[0111] CN103041804A discloses an aromatic hydrocarbon hydrogenation catalyst comprising a silica-alumina support and a hydrogenation-active metal component supported on the silica-alumina support. The silica-alumina support, measured at 200°C, shows a pyridine infrared ratio of β-acid to L-acid of 0.085–0.1. The hydrogenation-active metal component is platinum and palladium, and the content of the hydrogenation-active metal component in the aromatic hydrocarbon hydrogenation catalyst is 0.1–5% by weight, based on the weight of the aromatic hydrocarbon hydrogenation catalyst and calculated as oxides.

[0112] More detailed methods for preparing the aforementioned catalysts are described in the aforementioned patent documents, which are also incorporated herein by reference as part of this disclosure.

[0113] In one embodiment, in step S5, the method and conditions for the hydrodewaxed oil to enter the second separation unit for the second separation treatment are conventional methods and conditions. For example, separation is performed by distillation, a method known in the art, which typically includes one or more flash distillation, atmospheric distillation, and vacuum distillation units to achieve the desired separation. The apparatus used for the separation treatment also has a conventional structure in the art.

[0114] A second aspect of this disclosure provides a system for producing lubricating oil base oils and industrial white oils, such as... Figure 1 As shown, the system includes a solvent deasphalting unit, a hydrocracking unit, a first separation unit, a catalytic dewaxing reaction unit, and a separation unit arranged in sequence.

[0115] The deasphalting unit is configured to perform solvent deasphalting and refining treatment on the residual oil to obtain deasphalted oil.

[0116] The hydrocracking unit includes a first hydrocracking catalyst, and the hydrocracking unit is configured to contact hydrogen, vacuum wax oil and deasphalted oil from the deasphalting unit with the first hydrocracking catalyst to carry out a first hydrocracking reaction to obtain hydrocracking product oil; wherein the first hydrocracking catalyst includes a hydrotreating catalyst, a hydrocracking catalyst and a hydrorefining catalyst.

[0117] The first separation unit is configured to perform a first separation process on the hydrocracking product oil from the hydrocracking unit to obtain naphtha, jet fuel, diesel oil and tail oil;

[0118] The catalytic dewaxing reaction unit includes a second catalyst, and the catalytic dewaxing reaction unit is configured to contact the tail oil from the first separation unit with the second hydrogenation catalyst to carry out a second hydrogenation reaction to obtain hydrogenated dewaxed oil; wherein the second hydrogenation catalyst includes a hydroisomerization catalyst and a post-hydrogenation refining catalyst;

[0119] The second separation unit is configured to perform a second separation process on the hydrodewaxed oil from the catalytic dewaxing reaction unit to obtain lubricating oil base oil and industrial white oil.

[0120] In a preferred embodiment, the hydrotreating catalyst, hydrocracking catalyst, and hydrorefining catalyst are sequentially arranged along the flow direction of the mixed feedstock in the hydrocracking unit. Preferably, a hydroprotective agent is also arranged upstream of the hydrotreating catalyst along the flow direction of the mixed feedstock in the hydrocracking unit. The volume ratio of the hydroprotective agent: hydrotreating catalyst: hydrocracking catalyst: hydrorefining catalyst is (5-30):(60-250):100:(30-150); preferably (10-25):(80-200):100:(50-100).

[0121] In a preferred embodiment, the hydroisomerization catalyst and the post-hydrogenation refining catalyst are sequentially arranged along the material flow direction in the catalytic dewaxing reaction unit; preferably, the content of the post-hydrogenation refining catalyst, based on the hydroisomerization catalyst, is 50-200% by volume, preferably 80-150% by volume.

[0122] In this disclosure, the apparatus used in the systems for producing lubricating base oils and industrial white oils are all conventionally selected structures in the art.

[0123] The present disclosure is further described in detail below through examples.

[0124] In the following examples and comparative examples, the catalysts used were sourced from the following sources:

[0125] The commercial brand name of the hydrorefining catalyst I is RN-410, which was purchased from Changling Catalyst Factory. Based on the total weight of the catalyst, its composition includes: molybdenum oxide not less than 26.5% by weight, nickel oxide not less than 4.2% by weight, and the remainder being aluminum oxide.

[0126] The commercial brand name of the hydrocracking catalyst II is RHC-131. It was purchased from Changling Catalyst Factory. Based on the total weight of the catalyst, its composition includes: tungsten oxide not less than 24.5% by weight, nickel oxide not less than 6.5% by weight, and the remainder is mesoporous silica-alumina and molecular sieves, with Y-type molecular sieves accounting for 5-10% by weight.

[0127] The commercial brand name of the hydrogenation protectant IV is RG-1. It was purchased from Changling Catalyst Factory. Based on the total weight of the catalyst, its composition includes: molybdenum oxide not less than 5.5% by weight, nickel oxide not less than 1.0% by weight, and the remainder being aluminum oxide.

[0128] The commercial brand name of the hydroisomerization catalyst V is RIW-2. It was purchased from Changling Catalyst Factory. Based on the total weight of the catalyst, its composition includes: platinum not less than 0.3% by weight, the remainder being molecular sieves and alumina. Based on the total weight of the catalyst, the molecular sieve content is 40% by weight.

[0129] The commercial brand name of the hydrogenation refining catalyst VI is RLF-20, which was purchased from Changling Catalyst Factory. Based on the total weight of the catalyst, its composition includes: platinum not less than 0.1 wt%, palladium not less than 0.2 wt%, and the remainder being amorphous silicon and aluminum.

[0130] The hydrorefining catalyst III in the comparative example is commercially available as RN-410, purchased from Changling Catalyst Factory. Based on the total weight of the catalyst, its composition includes: molybdenum oxide not less than 26.5% by weight, nickel oxide not less than 4.2% by weight, and the remainder being aluminum oxide.

[0131] Preparation Example 1

[0132] The hydrorefining catalyst III used in the examples was prepared by the following method:

[0133] Weigh 2000g of aluminum hydroxide powder (product of Changling Catalyst Factory), extrude it into clover-shaped strips with an outer circle diameter of 1.5 mm on an extruder, dry the wet strips at 120℃ for 8 hours, and calcine them at 620℃ for 3 hours under air circulation to obtain the carrier.

[0134] Weigh 100g of the above-mentioned carrier, soak it in 102ml of an aqueous solution containing 24.4g of magnesium nitrate for 1.5 hours, dry it at 120℃ for 4 hours, and then calcine it at 370℃ for 4 hours under air circulation to obtain a magnesium-containing carrier.

[0135] Weigh 228.6 g of basic nickel carbonate, 176 g of ammonium carbonate, and 8.7 g of molybdenum trioxide, place them in a beaker, add 300 g of concentrated ammonia, stir and dissolve, and dilute with deionized water to 538.8 mL to obtain a co-impregnation solution containing nickel and molybdenum.

[0136] The magnesium-containing support was impregnated with the co-impregnation solution for 1.5 hours at a liquid-to-solid volume ratio of 2:1, then filtered, and the wet strip was dried at 150°C for 4 hours. 95 mL of co-impregnation solution was added to the filtrate, and then a second impregnation was performed. After 2 hours, the mixture was filtered, dried at 100°C for 6 hours, and calcined at 250°C for 4 hours to obtain the hydrorefining catalyst III.

[0137] Its weight composition is: 2.6 wt% magnesium oxide, 2.0 wt% molybdenum oxide, 27.2 wt% nickel oxide, and the balance is γ-Al2O3.

[0138] Preparation Example 2

[0139] Hydrogen refining catalyst was prepared according to Preparation Example 1. The difference between this comparative example and Preparation Example 1 is that magnesium is not introduced, and the support is directly immersed in a co-impregnation solution containing nickel and molybdenum for impregnation; thus, hydrogen refining catalyst D-III was prepared.

[0140] Its weight composition is: 2.0 wt% molybdenum oxide, 27.2 wt% nickel oxide, and the balance is γ-Al2O3.

[0141] Example 1

[0142] according to Figure 1 The process shown produces lubricating oil base oil and industrial white oil. The residue oil is a vacuum distillation bottom oil, and its properties are listed in Table 1. The properties of the vacuum distillation wax oil are listed in Table 3.

[0143] (1) In the solvent deasphalting unit:

[0144] The residue from the extraction tower with a distillation range >520℃ and C3 alkane (propane) were introduced from the top and bottom of the extraction tower, respectively, and subjected to countercurrent contact within the tower for solvent deasphalting and refining of the residue. Operating conditions included: top temperature of the extraction tower 40℃, pressure 4.0 MPa, and solvent ratio 6.0 (v / v). The yield and properties of the deasphalted oil obtained after extraction are listed in Table 2.

[0145] (2) In the hydrocracking unit:

[0146] The catalyst is a graded combination of catalyst IV (hydrogenation protectant), I (hydrogenation treatment catalyst), II (hydrocracking catalyst), and III (hydrorefining catalyst). The hydrocracking reaction unit can be selected from three reactors in series, two reactors in series, or a single reactor. In this embodiment, it is a two reactors in series.

[0147] Among them, the catalyst IV:I:II:III = 25:100:120:50 (packing volume ratio); the properties of the hydrogenation feed, reaction conditions, and the yield and properties of the bottom product obtained by distillation at >380℃ (based on the hydrogenation feed oil) are listed in Tables 3 to 4.

[0148] (3) In the catalytic dewaxing reaction unit:

[0149] The isomer catalyst V and the post-purification catalyst VI used in the catalytic dewaxing reaction unit adopt a two-reaction-one-stage series mode, wherein the ratio of catalyst V (hydrogenation isomer catalyst) to VI (hydrogenation post-purification catalyst) is 1:1 (volume ratio).

[0150] The conditions for the hydroisomerization catalytic reaction included: a temperature of 330°C, a pressure of 15 MPa, and a liquid hourly space velocity of 0.8 h⁻¹. -1 The hydrogen-to-oil volume ratio was 600; the conditions for the purification reaction after hydrogenation included: a temperature of 330℃, a pressure of 15 MPa, and a liquid hourly space velocity of 0.8 h⁻¹. -1 The hydrogen-to-oil volume ratio was 600. The yield and properties of the product oil obtained by distillation are listed in Tables 5 and 6.

[0151] According to the analysis data, the method provided in this disclosure can produce lubricating oil base oil with a viscosity index greater than 120 (HVI III) and a pour point less than -24°C, which can also be used as No. 32 Group II industrial white oil product; at the same time, it can produce No. 100 Group II industrial white oil product with a viscosity index of 127, which can be used as HVI III 12cst base oil product.

[0152] Table 1 Properties of vacuum residue

[0153] crude oil vacuum residue <![CDATA[Density (20 °C) / g·cm -3 > 0.965 <![CDATA[100℃ kinematic viscosity / mm 2 ·s -1 > 43.10 Residual char / % by weight 9.81 Sulfur content / weight % 3.5 Nitrogen content / weight % 0.36 Asphalt content / weight % 3.6

[0154] Table 2 Properties of Deasphalted Oil

[0155]

[0156]

[0157] Table 3 Properties of Hydrocracking Feed

[0158] Brand Stress-relieving wax oil Deasphalted oil Mixed feed Mixing ratio / weight% 85 15 100 <![CDATA[Density (20 °C) / g·cm -3 > 0.9225 0.9476 0.9288 <![CDATA[Kinematic viscosity / mm 2 ·s -1 > 100℃ 9.45 38.78 13.45 Color / Number 4.0 8.0 6.5 Pour point / °C 34 56 38 Residual char / % by weight 0.02 5.8 0.89 Sulfur content / weight % 1.8 2.6 1.92 Nitrogen content / weight % 0.12 0.14 0122 <![CDATA[Acid value / mgKOH·g -1 > 0.10 0.42 0.15

[0159] Table 4 Results of hydrocracking unit reaction

[0160] Reaction conditions Hydrogen partial pressure / MPa 15.0 <![CDATA[Hydrotreating / Cracking / Hydrofining Space Velocity / h -1 > 0.8 / 0.67 / 1.6 Average reaction temperature in hydrotreating / cracking / hydrorefining / °C 375 / 380 / 380 Hydrogen-to-oil volume ratio 1000：1 reaction results Naphtha yield / weight % 21.3 Jet fuel yield / weight % 15.8 Diesel yield / weight % 29.6 Residual oil yield / weight / % 33.6 Properties of hydrotreated tail oil at >390℃ <![CDATA[Density (20 °C) / g·cm -3 > 0.866 <![CDATA[100℃ kinematic viscosity / mm 2 ·s -1 > 6.75 Sulfur content / μg / g 15 Nitrogen content / μg / g 2 Saipo Special 16 Aromatic content / weight % 1.6 Saturated hydrocarbon content / weight % 98.4

[0161] Table 5. Hydroisomerization Dewaxing Reaction Conditions

[0162] Reaction conditions Hydrogen partial pressure / MPa 15.0 <![CDATA[Hydroisomerization / Post-refining Space Velocity per Hour -1 > 0.8 / 0.8 Average reaction temperature at ℃ for hydroisomerization / post-purification 330 / 210 Hydrogen-to-oil volume ratio 600:1 reaction results Naphtha yield / weight % 7.38 Diesel yield / weight % 11.23 2cst base oil yield / weight % 9.00 4cst base oil yield / weight % 11.46 6cst base oil yield / weight % 25.92 12cst base oil yield / weight % 32.21

[0163] Table 6 Properties of Base Oil Products

[0164] project 4CST base oil 6cst base oil 12cst base oil <![CDATA[Viscosity at 40℃ / (mm 2 / s)]]> 19.48 29.58 94.75 <![CDATA[Viscosity at 100℃ / (mm 2 / s)]]> 4.174 5.506 12.52 Viscosity Index 118 125 127 Pour point / ℃ <-27 <-24 <-21 Flash point / °C 216 >220 >220 Aromatic content / weight % <0.1 <0.1 <0.2 Color / Seybert +30 +30 +30

[0165] Comparative Example 1

[0166] Referring to the process flow of Example 1, the difference between this comparative example and Example 1 is that: no hydrorefining catalyst is added to the hydrocracking unit; the commercial brand name of hydroprotectant IV is RG-1; the commercial brand name of hydrorefining catalyst I is RN-410; and the commercial brand name of hydrocracking catalyst II is RHC-131. Among them, the ratio of catalyst IV:I:II is 25:100:120 (volume ratio).

[0167] The commercial brand name of the hydrocracking catalyst V is RIW-2, and the commercial brand name of the post-hydrocracking refining catalyst is RLF-20. The catalyst volume ratio V:VI = 1:1. The properties of the feedstock are the same as in Table 3. The operation of the hydrocracking reaction unit and the catalytic dewaxing unit is listed in Tables 7 and 8, and the properties of the products are listed in Table 9.

[0168] Table 7 Results of hydrocracking unit reactions

[0169] Reaction conditions Hydrogen partial pressure / MPa 15.0 <![CDATA[Hydrotreating / Cracking Space Velocity / h -1 > 0.8 / 0.67 Average reaction temperature of hydrotreating / cracking / °C 375 / 380 Hydrogen-to-oil volume ratio 1000 reaction results Naphtha yield / weight % 22.3 Jet fuel yield / weight % 14.8 Diesel yield / weight % 30.4 Residual oil yield / weight % 32.8 Properties of hydrotreated tail oil at >380℃ <![CDATA[Density (20 °C) / g·cm －3 > 0.872 <![CDATA[100℃ kinematic viscosity / mm 2 ·s －1 > 6.82 Sulfur content / μg / g 10 Nitrogen content / μg / g 2 Saipo Special <-16 Aromatic content / % 5.2 Saturated hydrocarbon content / weight % 94.8

[0170] Table 8. Hydroisomerization Dewaxing Reaction Conditions

[0171] Reaction conditions Hydrogen partial pressure / MPa 15.0 <![CDATA[Hydroisomerization / Post-refining Space Velocity per Hour -1 > 0.8 / 0.8 Average reaction temperature at ℃ for hydroisomerization / post-purification 330 / 210 Hydrogen-to-oil volume ratio 600:1 reaction results Naphtha yield / weight % 9.24 Diesel yield / weight % 11.13 2cst base oil yield / weight % 9.2 4cst base oil yield / weight % 10.86 6cst base oil yield / weight % 24.74 12cst base oil yield / weight % 31.45

[0172] Table 9 Properties of Base Oil Products

[0173]

[0174]

[0175] Comparing Comparative Example 1 with Example 1, it can be seen that Example 1, which uses the method provided in this disclosure, employs a hydrorefining catalyst in the hydrocracking unit. The hydrocracking product obtained from the hydrocracking unit of Example 1 has a lower aromatic content and a higher saturated hydrocarbon content, resulting in a better quality base oil product (e.g., higher viscosity index, lower aromatic content, and higher Seybert number).

[0176] Example 2

[0177] The process is the same as in Example 1. The difference between this example and Example 1 is that the hydrorefining catalyst III is replaced with a commercially available hydrorefining catalyst, RN-410.

[0178] The commercial brand names for hydrotreating protectant IV are RG-1, hydrorefining catalyst I are RN-410, hydrocracking catalyst II are RHC-131, and hydrorefining catalyst III are RN-410, with a volume ratio of IV:I:II:III = 25:100:120:50. The commercial brand name for hydrotreating catalytic dewaxing catalyst V is RIW-2, and the commercial brand name for post-hydrotreating refining catalyst is RLF-20, with a catalyst volume ratio of V:VI = 1:1.

[0179] The properties of the raw materials are the same as in Table 3. The operations of the hydrocracking reaction unit and the catalytic dewaxing unit are listed in Tables 10 and 11. The properties of the products are listed in Table 12.

[0180] Table 10 Results of Hydrocracking Unit Reactions

[0181]

[0182]

[0183] Table 11 Hydroisomerization Dewaxing Reaction Conditions

[0184] Reaction conditions Hydrogen partial pressure / MPa 15.0 <![CDATA[Hydroisomerization / Post-refining space velocity per hour -1 > 0.8 / 0.8 Average reaction temperature at ℃ for hydroisomerization / post-purification 330 / 210 Hydrogen-to-oil volume ratio 600:1 reaction results Naphtha yield / weight % 9.48 Diesel yield / weight % 11.13 2cst base oil yield / weight % 9.12 4cst base oil yield / weight % 11.44 6cst base oil yield / weight % 26.05 12cst base oil yield / weight % 30.18

[0185] Table 12 Properties of Base Oil Products

[0186]

[0187]

[0188] Comparing Example 2 with Example 1, it can be seen that the hydrorefining catalyst used in Example 1 contains three active metal elements: nickel, molybdenum, and magnesium. The hydrocracking unit of Example 1 produces hydro-oil with lower aromatic content and higher saturated hydrocarbon content (above 98% by weight), resulting in better quality base oil products (such as higher viscosity index, lower aromatic content, and higher Seybert number).

[0189] Comparative Example 2

[0190] Referring to the process of Example 1, the difference between this comparative example and Example 1 is that: no residual oil is introduced, and no solvent deasphalting refining treatment is performed; only vacuum wax oil is introduced as a raw material into the hydrocracking unit; the rest of the process and conditions are the same as in Example 1.

[0191] The properties of the raw materials are the same as in Table 3. The operations of the hydrocracking reaction unit and the catalytic dewaxing unit are listed in Tables 13 and 14. The properties of the products are listed in Table 15.

[0192] Table 13 Results of hydrocracking unit reaction

[0193] Reaction conditions Hydrogen partial pressure / MPa 15.0 <![CDATA[Hydrotreating / Cracking / Hydrofining Space Velocity (volumetric) / h -1 > 0.8 / 0.67 / 1.6 Average reaction temperature in hydrotreating / cracking / hydrorefining / °C 375 / 380 / 380 Hydrogen-to-oil volume ratio 1000:1 reaction results Naphtha yield / weight % 26.4 Jet fuel yield / weight % 16.2 Diesel yield / weight % 33.2 Residual oil yield / weight / % 24.4 Properties of hydrotreated tail oil at >390℃ <![CDATA[Density (20 °C) / g·cm －3 > 0.854 <![CDATA[Kinematic viscosity at 100 °C / mm 2 ·s －1 > 5.38 Sulfur content / μg / g 10 Nitrogen content / μg / g 2 Saipo Special 20 Aromatic content / weight % 1.2 Saturated hydrocarbon content / weight % 98.8

[0194] Table 14 Conditions for Hydroisomerization Dewaxing Reaction

[0195] Reaction conditions Hydrogen partial pressure / MPa 15.0 <![CDATA[Hydroisomerization / Post-refining space velocity / h -1 > 0.8 / 0.8 Average reaction temperature at ℃ for hydroisomerization / post-purification 330 / 210 Hydrogen-to-oil volume ratio 600:1 reaction results Naphtha yield / weight % 9.46 Diesel yield / weight % 10.55 2cst base oil yield / weight % 9.32 4cst base oil yield / weight % 13.26 6cst base oil yield / weight % 49.48 10cst base oil yield / weight % 6.6

[0196] Table 15 Properties of Base Oil Products

[0197] project 4CST base oil 6cst base oil 10cst base oil <![CDATA[Viscosity at 40°C / (mm 2 / s)]]> 19.58 30.36 59.38 <![CDATA[Viscosity at 100 °C / (mm 2 / s)]]> 4.08 5.52 8.82 Viscosity Index 107 120 121 Pour point / ℃ <-27 <-24 <-12 Flash point / °C 216 >220 >220 Aromatic content / weight % <1 <1 <1.5 Color / Seybert +30 +22 +6

[0198] Comparing Comparative Example 2 with Example 1, it can be seen that Example 1, which uses the method provided in this disclosure, introduces residual oil into the process and performs solvent deasphalting and refining treatment. Example 1 can simultaneously produce high viscosity index base oil and high viscosity industrial white oil, thereby improving the quality of oil products.

[0199] Example 3

[0200] Referring to the process of Example 1, the difference between this comparative example and Example 1 is that the hydrorefining catalyst III is replaced with the hydrorefining catalyst D-III obtained in Example 2; the rest of the process and conditions are the same as in Example 1.

[0201] The properties of the raw materials are the same as in Table 3. The operations of the hydrocracking reaction unit and the catalytic dewaxing unit are listed in Tables 16 and 17. The properties of the products are listed in Table 18.

[0202] Table 16 Results of Hydrocracking Unit Reactions

[0203] Reaction conditions Hydrogen partial pressure / MPa 15.0 <![CDATA[Hydrotreating / Cracking / Hydrofining Volumetric Space Velocity / h -1 > 0.8 / 0.67 / 1.6 Average reaction temperature in hydrotreating / cracking / hydrorefining / °C 375 / 380 / 380 Hydrogen-to-oil volume ratio 1000 reaction results Naphtha yield / weight % 22.4 Jet fuel yield / weight % 13.2 Diesel yield / weight % 31.3 Residual oil yield / weight / % 33.6 Properties of hydrotreated tail oil at >390℃ <![CDATA[Density (20 °C) / g·cm －3 > 0.864 <![CDATA[100℃ kinematic viscosity / mm 2 ·s －1 > 6.76 Sulfur content / μg / g 10 Nitrogen content / μg / g 2 Saipo Special 0 Aromatic content / weight % 3.4 Saturated hydrocarbon content / weight % 96.6

[0204] Table 17 Hydroisomerization Dewaxing Reaction Conditions

[0205] Reaction conditions Hydrogen partial pressure / MPa 15.0 <![CDATA[Hydroisomerization / Post-refining Space Velocity per Hour -1 > 0.8 / 0.8 Average reaction temperature at ℃ for hydroisomerization / post-purification 330 / 210 reaction results Naphtha yield / weight % 9.44 Diesel yield / weight % 11.03 2cst base oil yield / weight % 9.16 4cst base oil yield / weight % 11.64 6cst base oil yield / weight % 26.26 12cst base oil yield / weight % 30.02

[0206] Table 18 Properties of Base Oil Products

[0207] project 4CST base oil 6cst base oil 12cst base oil <![CDATA[Viscosity at 40°C / (mm 2 / s)]]> 19.36 29.82 97.04 <![CDATA[Viscosity at 100℃ / (mm 2 / s)]]> 4.159 5.543 12.53 Viscosity Index 118 124 124 Pour point / ℃ <-27 <-24 <-21 Flash point / °C 216 >220 >220 Aromatic content / weight % <0.1 <0.1 <1 Color / Seybert +30 +28 +22

[0208] Comparing Example 3 with Example 1, it can be seen that the hydrorefining catalyst used in Example 1 contains three active metal elements: nickel, molybdenum, and magnesium. The hydrocracking unit of Example 1 produces hydro-oil with lower aromatic content and higher saturated hydrocarbon content (above 98% by weight), resulting in better quality base oil products (such as higher viscosity index, lower aromatic content, and higher Seybert number).

[0209] Examples 4-6

[0210] The process is the same as in Example 1, except that the reaction conditions of the hydrocracking unit listed in Table 19 or the hydroisomerization dewaxing reaction conditions listed in Table 20 are followed.

[0211] The properties of the raw materials are the same as in Table 3. The operations of the hydrocracking reaction unit and the catalytic dewaxing unit are listed in Tables 19 and 20, and the properties of the products are listed in Table 21.

[0212] Table 19 Results of Hydrocracking Unit Reactions

[0213]

[0214]

[0215] Table 20 Hydroisomerization Dewaxing Reaction Conditions

[0216]

[0217] Table 21 Properties of Base Oil Products

[0218]

[0219] According to Tables 19 to 21 above, it can be seen that:

[0220] Comparing Example 4 with Example 1, Example 1 was carried out in the process of producing lubricating oil base oil and industrial white oil according to the catalyst loading volume ratio of the preferred embodiment of this disclosure (the volume ratio of hydroprotectant: hydrotreatment catalyst: hydrocracking catalyst: hydrorefining catalyst is 10-25:100:80-200:50-100). Comparing Example 5 with Example 1, Example 1 was processed in the hydrocracking unit according to the process conditions of the preferred embodiment of this disclosure in the process of producing lubricating oil base oil and industrial white oil. Comparing Example 6 with Example 1, Example 1 was processed in the catalytic dewaxing reaction unit according to the process conditions of the preferred embodiment of this disclosure in the process of producing lubricating oil base oil and industrial white oil. Compared with Examples 4-6, the base oil product obtained by Example 1 has better quality (e.g., higher viscosity index, lower aromatic content, and higher Seybert number).

[0221] The preferred embodiments of this disclosure have been described in detail above. However, this disclosure is not limited to the specific details of the above embodiments. Within the scope of the technical concept of this disclosure, various simple modifications can be made to the technical solutions of this disclosure, and these simple modifications all fall within the protection scope of this disclosure.

[0222] It should also be noted that the various specific technical features described in the above embodiments can be combined in any suitable manner without contradiction. To avoid unnecessary repetition, this disclosure will not describe the various possible combinations separately.

[0223] Furthermore, various different embodiments of this disclosure can be combined in any way, as long as they do not violate the spirit of this disclosure, they should also be regarded as the content disclosed in this disclosure.

Claims

1. A method for producing lubricating oil base oil and industrial white oil, characterized in that, Includes the following steps: S1. The residual oil is fed into the solvent deasphalting unit for solvent deasphalting and refining treatment to obtain deasphalted oil; S2. Hydrogen, vacuum wax oil, and the deasphalted oil are introduced into a hydrocracking unit and contacted with a first hydrocracking catalyst to carry out a first hydrocracking reaction, yielding hydrotreated oil. The first hydrocracking catalyst includes a hydrotreatment catalyst, a hydrocracking catalyst, and a hydrorefining catalyst. The hydrorefining catalyst includes a third support and a third active metal component supported on the third support. The third support is selected from alumina and / or silica. The third active metal component is nickel, molybdenum, and magnesium. S3. The hydrogenated oil is fed into the first separation unit for the first separation process to obtain naphtha, jet fuel, diesel oil and tail oil; S4. The tail oil is brought into the catalytic dewaxing reaction unit and contacted with the second hydrogenation catalyst to carry out the second hydrogenation reaction, thereby obtaining hydrogenated dewaxed oil. The second hydrogenation catalyst includes a hydrogenation isomerization catalyst and a post-hydrogenation refining catalyst. S5. The hydrodewaxed oil is fed into the second separation unit for a second separation process to obtain lubricating oil base oil and industrial white oil. Along the flow direction of the mixed feedstock in the hydrocracking unit, the hydrotreatment catalyst, the hydrocracking catalyst, and the hydrorefining catalyst are arranged sequentially; step S2 includes: The vacuum wax oil and the deasphalted oil are mixed and then introduced into the hydrocracking unit, and the mixed feedstock is first contacted with the hydrocracking catalyst to carry out a hydrocracking reaction. Then, it is contacted with the hydrocracking catalyst to carry out a hydrocracking reaction; then, it is contacted with the hydrorefining catalyst to carry out a hydrorefining reaction to obtain the hydrotreated oil; along the flow direction of the mixed feedstock in the hydrocracking unit, a hydrotreating protectant is also provided upstream of the hydrotreating catalyst; the volume ratio of the hydrotreating protectant: hydrotreating catalyst: hydrocracking catalyst: hydrorefining catalyst is (5~30):100:(60~250):(30~150); In step S2, based on the total weight of the hydrorefining catalyst, the content of the third active metal in the form of oxides is 0.5-2.6 wt% for magnesium oxide, 1.5-5.5 wt% for molybdenum oxide, 20-28 wt% for nickel oxide, and 64-78 wt% for the third support.

2. The method according to claim 1, characterized in that, In step S1, the conditions for the solvent deasphalting and refining treatment include: In the extraction tower, the volume ratio of solvent to residual oil is (2~10):1, the temperature at the top of the extraction tower is 20~150℃, and the pressure is 2~6MPa.

3. The method according to claim 2, characterized in that, In step S1, the conditions for solvent deasphalting and refining treatment include: a solvent to residual oil volume ratio of (3~8):1, an extraction tower top temperature of 30~120℃, and a pressure of 3~5MPa.

4. The method according to claim 2, characterized in that, The solvent is selected from one or more of hydrocarbons with 3 to 7 carbon atoms, condensate oil, light naphtha, and gasoline.

5. The method according to claim 4, characterized in that, The solvent includes propane.

6. The method according to claim 4, characterized in that, The solvent includes propane and one or more selected from ethane, propylene, butane and pentane.

7. The method according to claim 5 or 6, characterized in that, The solvent contains 80-100% propane by weight.

8. The method according to claim 7, characterized in that, The solvent contains 90-100% propane by weight.

9. The method according to claim 8, characterized in that, The solvent contains 95-100% propane by weight.

10. The method according to claim 2, characterized in that, The solvent deasphalting and refining process results in the deasphalted oil having a carbon residue value of less than 10% by weight.

11. The method according to claim 10, characterized in that, The solvent deasphalting and refining process reduces the carbon residue of the deasphalted oil to below 6% by weight.

12. The method according to claim 1, characterized in that, The residue oil is selected from vacuum residue oil and / or atmospheric residue oil.

13. The method according to claim 1, characterized in that, In step S2, the volume ratio of the hydrogenation protective agent: hydrogenation treatment catalyst: hydrocracking catalyst: hydrorefining catalyst is (10~25):100:(80~200):(50~100).

14. The method according to claim 1, characterized in that, In step S2, the volume ratio of the depressurized wax oil to the deasphalted oil is (3~20):

1.

15. The method according to claim 14, characterized in that, In step S2, the volume ratio of the depressurized wax oil to the deasphalted oil is (5~10):

1.

16. The method according to claim 1, characterized in that, In step S2, the carbon residue of the mixture of the vacuum wax oil and the deasphalted oil is no more than 2% by weight.

17. The method according to claim 16, characterized in that, In step S2, the carbon residue of the mixture of the depressurized wax oil and the deasphalted oil is not greater than 1% by weight.

18. The method according to claim 1, characterized in that, In step S2, the processing conditions of the hydrocracking unit include: The hydrogenation reaction was carried out at temperatures of 300–450 °C, hydrogen partial pressures of 8–25 MPa, and volume hourly space velocities of 0.3–2.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (300~2500):1; The hydrocracking reaction is carried out at temperatures of 320–450 °C, hydrogen partial pressures of 8–25 MPa, and volume hourly space velocities of 0.3–2.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (300~2500):1; The hydrogenation purification reaction is carried out at temperatures ranging from 280 to 420°C, with hydrogen partial pressures ranging from 8 to 25 MPa and volume hourly space velocities ranging from 0.3 to 2.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (300~2500):

1.

19. The method according to claim 18, characterized in that, In step S2, the processing conditions of the hydrocracking unit include: The hydrogenation reaction was carried out at a temperature of 320–420 °C, a hydrogen partial pressure of 10–20 MPa, and a volume hourly space velocity of 0.4–2.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is (400~2000):1; The hydrocracking reaction is carried out at temperatures of 340–420 °C, hydrogen partial pressures of 10–20 MPa, and volume hourly space velocities of 0.4–2.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is (400~2000):1; The hydrogenation purification reaction is carried out at a temperature of 300–400 °C, a hydrogen partial pressure of 10–20 MPa, and a volume hourly space velocity of 0.4–2.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (400~2000):

1.

20. The method according to claim 1, characterized in that, In step S2, the hydrogenation catalyst includes a first support, an active metal component, an optional first auxiliary agent, and an optional organic additive. The first carrier is selected from one or more of alumina, silicon dioxide, titanium dioxide, magnesium oxide, zirconium oxide, thorium oxide, beryllium oxide, natural zeolite, and clay; the active metal component includes a first metal component and a second metal component; the first metal component is selected from nickel and / or cobalt; the second metal component is selected from molybdenum and / or tungsten; the first additive is selected from one or more of fluorine, boron, and phosphorus. The organic additives are selected from oxygen-containing organic compounds and / or nitrogen-containing organic compounds.

21. The method according to claim 20, characterized in that, The first carrier is selected from alumina and / or silicon oxide-alumina.

22. The method according to claim 20, characterized in that, The oxygen-containing organic compound is selected from organic alcohols and / or organic acids; the nitrogen-containing organic compound is selected from one or more organic amines.

23. The method according to claim 22, characterized in that, The oxygen-containing organic compound is selected from one or more of ethylene glycol, glycerol, polyethylene glycol, diethylene glycol, butanediol, acetic acid, maleic acid, oxalic acid, aminotriacetic acid, 1,2-cyclohexanediaminetetraacetic acid, citric acid, tartaric acid, and malic acid; the nitrogen-containing organic compound is selected from one or more of ethylenediamine, EDTA, and their ammonium salts.

24. The method according to claim 20, characterized in that, The first carrier is γ-alumina; the active metal component is tungsten oxide and nickel oxide; and the first additive is fluorine.

25. The method according to claim 24, characterized in that, Based on the total weight of the hydrotreating catalyst, the nickel oxide content is 1-5% by weight, the tungsten oxide content is 12-35% by weight, the fluorine content is 1-9% by weight, and the balance is γ-alumina.

26. The method according to claim 1, characterized in that, In step S2, the hydrocracking catalyst includes a second support and one or more of group VIII and group VIB metals supported on the second support.

27. The method according to claim 26, characterized in that, The second carrier comprises a Y-type molecular sieve and an amorphous composite oxide; the amorphous composite oxide is selected from at least two of silicon oxide, aluminum oxide, titanium oxide and zirconium oxide.

28. The method according to claim 27, characterized in that, Based on the total weight of the hydrocracking catalyst, the content of group VIII metals is 2-8% by weight, the content of group VIB metals is 12-33% by weight, the content of Y-type molecular sieve is 1-30% by weight, and the content of amorphous composite oxides is 50-80% by weight, wherein the group VIII metals and group VIB metals are in oxide form.

29. The method according to claim 1, characterized in that, The hydrogenated oil obtained in step S2 contains more than 80% saturated hydrocarbons by weight.

30. The method according to claim 29, characterized in that, The saturated hydrocarbon content in the hydrogenated oil obtained in step S2 is 90-100% by weight.

31. The method according to claim 30, characterized in that, The saturated hydrocarbon content in the hydrogenated oil obtained in step S2 is 98-100% by weight.

32. The method according to claim 1, characterized in that, The tail oil obtained in step S3 has a sulfur content of less than 50 μg / g, a nitrogen content of less than 10 μg / g, a distillation range of more than 300℃, and a color greater than 16 Cépôt.

33. The method according to claim 32, characterized in that, The tail oil obtained in step S3 has a sulfur content of less than 20 μg / g, a nitrogen content of less than 5 μg / g, a distillation range of more than 320℃, and a color greater than 14 Cépôt.

34. The method according to claim 33, characterized in that, The tail oil obtained in step S3 has a sulfur content of less than 10 μg / g, a nitrogen content of less than 2 μg / g, a distillation range of more than 370℃, and a color greater than 12 Cépôt.

35. The method according to claim 1, characterized in that, In step S4, the hydroisomerization catalyst and the post-hydrogenation refining catalyst are sequentially arranged along the material flow direction in the catalytic dewaxing reaction unit, so that after the tail oil enters the catalytic dewaxing reaction unit, it first contacts the hydroisomerization catalyst to carry out a hydroisomerization catalytic reaction; then it contacts the post-hydrogenation refining catalyst to carry out a post-hydrogenation refining reaction, thereby obtaining the hydrodewaxed oil.

36. The method according to claim 35, characterized in that, The content of the hydrogenated refined catalyst is 50-200% by volume, based on the hydrogenation isomerization catalyst.

37. The method according to claim 36, characterized in that, The content of the hydrogenated refined catalyst is 80-150% by volume, based on the hydrogenation isomerization catalyst.

38. The method according to claim 35, characterized in that, In step S4, the reaction conditions in the catalytic dewaxing reaction unit include: The hydroisomerization catalytic reaction is carried out at temperatures of 280–400 °C, pressures of 3–20 MPa, and liquid hourly space velocities of 0.4–2.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is (300~1200):1; The purification reaction after hydrogenation is carried out at a temperature of 150–300 °C, a pressure of 3–20 MPa, and a liquid hourly space velocity of 0.4–2.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is (300~1200):

1.

39. The method according to claim 38, characterized in that, In step S4, the reaction conditions in the catalytic dewaxing reaction unit include: The hydroisomerization catalytic reaction is carried out at a temperature of 300–380 °C, a pressure of 8–18 MPa, and a liquid hourly space velocity of 0.5–1.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (400~1000):1; The purification reaction after hydrogenation is carried out at a temperature of 180–250 °C, a pressure of 8–18 MPa, and a liquid hourly space velocity of 0.5–1.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is (400~1000):

1.

40. The method according to claim 1, characterized in that, In step S4, the hydroisomerization catalyst comprises a mesoporous molecular sieve, an inorganic oxide, and a fourth active metal component.

41. The method according to claim 40, characterized in that, The mesoporous molecular sieve is a one-dimensional elliptical pore structure with a short axis of 4.2~4.8 Å and a long axis of 5.4~7.0 Å.

42. The method according to claim 41, characterized in that, The mesoporous molecular sieves are selected from one or more of ZSM-22, Nu-10, Theta-1, ISI-1, ZSM-23, SAPO-11, SAPO-31 and SAPO-41 molecular sieves.

43. The method according to claim 42, characterized in that, The mesoporous molecular sieve is ZSM-22 molecular sieve.

44. The method according to claim 40, characterized in that, The fourth active metal component is selected from one or more of cobalt, nickel, ruthenium, rhodium, palladium, osmium, iridium, platinum, molybdenum and tungsten.

45. The method according to claim 44, characterized in that, The fourth active metal component is platinum.

46. ​​The method according to claim 40, characterized in that, The inorganic oxide is selected from aluminum oxide and / or silicon oxide.

47. The method according to claim 40, characterized in that, Based on the total weight of the hydroisomerization catalyst, the content of the mesoporous molecular sieve is 30-70% by weight, the content of the inorganic oxide is 30-70% by weight, and the content of the fourth active metal component in reduced state is 0.2-1% by weight.

48. The method according to claim 1, characterized in that, The hydrogenation refining catalyst comprises a silicon-aluminum support and a fifth active metal component supported on the silicon-aluminum support.

49. The method according to claim 48, characterized in that, Based on the weight of the silicon-aluminum carrier, the silicon-aluminum carrier comprises 16-20% by weight silicon (calculated as oxide) and 78-82% by weight aluminum (calculated as oxide).

50. The method according to claim 48, characterized in that, The ratio of pyridine β-acid to L-acid measured at 200℃ on the silica-alumina support was 0.06~0.

085.

51. The method according to claim 48, characterized in that, The fifth active metal component is selected from platinum and / or palladium.

52. The method according to claim 51, characterized in that, When the fifth active metal component is platinum and palladium, the content of reduced palladium is 0.1-5% by weight, based on the total weight of the fifth active metal component (calculated as oxides). The content of reduced platinum is 0.1~5% by weight.

53. The method according to claim 52, characterized in that, When the fifth active metal component is platinum and palladium, the content of reduced palladium is 0.2 to 2% by weight, based on the total weight of the fifth active metal component calculated as oxides; and the content of reduced platinum is 0.2 to 2% by weight.

54. A system for the method of producing lubricating oil base oil and industrial white oil as described in claim 1, characterized in that, The system includes a solvent deasphalting unit, a hydrocracking unit, a first separation unit, a catalytic dewaxing reaction unit, and a separation unit, which are connected in sequence. The deasphalting unit is configured to perform solvent deasphalting and refining treatment on the residual oil to obtain deasphalted oil. The hydrocracking unit includes a first hydrocracking catalyst, and the hydrocracking unit is configured to contact hydrogen, vacuum wax oil and deasphalted oil from the deasphalting unit with the first hydrocracking catalyst to carry out a first hydrocracking reaction to obtain hydrocracking product oil; wherein the first hydrocracking catalyst includes a hydrotreating catalyst, a hydrocracking catalyst and a hydrorefining catalyst. The first separation unit is configured to perform a first separation process on the hydrocracking product oil from the hydrocracking unit to obtain naphtha, jet fuel, diesel oil and tail oil; The catalytic dewaxing reaction unit includes a second hydrogenation catalyst, and the catalytic dewaxing reaction unit is configured to contact the tail oil from the first separation unit with the second hydrogenation catalyst to carry out a second hydrogenation reaction to obtain hydrodewaxed oil; wherein the second hydrogenation catalyst includes a hydroisomerization catalyst and a post-hydrogenation refining catalyst; The second separation unit is configured to perform a second separation process on the hydrodewaxed oil from the catalytic dewaxing reaction unit to obtain lubricating oil base oil and industrial white oil.

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