A method and system for producing a lubricating oil base oil

Abstract

The application discloses a production method and a production system of lubricating oil base oil, which first fractionates raw materials to obtain light lubricating oil materials and heavy lubricating oil materials, then the light lubricating oil materials enter a first reaction zone to respectively perform adsorption and isomerization and pour point depressing reactions, and 4# base oil and 6# base oil products are obtained after the reaction products are separated; the heavy lubricating oil materials enter a second reaction zone to respectively perform adsorption and isomerization and pour point depressing reactions, and 6# base oil and 8# base oil products are obtained after the reaction products are separated. The application adopts a segmented feeding mode, first fractionates raw materials, and makes the light lubricating oil materials and the heavy lubricating oil materials respectively react under suitable conditions, so that the problem that the pour point and the viscosity index cannot be considered simultaneously is solved.

Description

TECHNICAL FIELD

[0001] The present application belongs to the technical field of lubricating oil, and particularly relates to a production method and a production system of lubricating oil base oil. BACKGROUND

[0002] At present, the overall crude oil in the world presents a development trend of inferiorization, so that the amount of crude oil suitable for producing lubricating oil gradually decreases. The lubricating oil base oil produced by the traditional solvent refining process cannot meet the increasingly strict environmental regulations and the higher performance requirements, and the high energy consumption and heavy pollution of the traditional process restrict its development and application. In recent years, the production technology of lubricating oil by hydrogenation method has developed very rapidly. The hydrogenation method process refers to a method for producing lubricating oil base oil by using a hydrogenation cracking process or a hydrogenation treatment-isomerization dewaxing-hydrogenation refining combined process, which has the advantages of great flexibility of raw materials, high base oil yield, good performance, and high economic value of by-products.

[0003] The technical problem existing in the hydrogenation isomerization dewaxing process is that when full-range or wide-range feedstock is used, the light and heavy lubricating oil components in the raw material are difficult to simultaneously meet the requirements of pour point and viscosity index. Generally, in order to make the pour point of the heavy lubricating oil component qualified, the light lubricating oil component is excessively isomerized, resulting in the loss of the viscosity index of the light lubricating oil component, so that it is difficult to produce API III light base oil products with a viscosity index higher than 120.

[0004] In the existing method, in order to prepare high-viscosity-index lubricating oil base oil products, some methods cut the raw material into narrow components, and then use the narrow fractions as the feedstock for hydrogenation isomerization dewaxing, so as to solve the problem of producing high-viscosity-index light lubricating oil base oil. Some methods also use full-range or wide-range feedstock to produce high-viscosity-index lubricating oil base oil by gradually isomerizing dewaxing and separating the products.

[0005] CN103289738A discloses a combined method for producing high-grade lubricating oil base oil by hydrogenation of hydrocracking tail oil. The hydrocracking tail oil is first subjected to vacuum fractionation to obtain No. 4 base oil material with a final boiling point ≤430℃ and No. 6 base oil material with an initial boiling point >430℃. Then, the two materials are subjected to hydrogenation isomerization dewaxing reaction and make-up refining reaction with hydrogen gas by switching the feedstock or by independent feeding. The reaction product is first subjected to gas-liquid separation to obtain hydrogen-rich gas and low-boiling oil. The low-boiling oil is sent to a atmospheric and vacuum distillation device to obtain dry gas and high-grade lubricating oil base oil. The produced base oil can meet the requirements of API II and III high-grade lubricating oil base oil. SUMMARY

[0006] The inventors of the present application found in the research process that long-chain isomeric alkanes and long-side-chain monocyclic naphthenes are ideal components for forming high-viscosity-index lubricating oil base oil. In addition to synthetic products such as Fischer-Tropsch synthesis oil (F-T oil), polyesters, etc., feedstocks for producing lubricating oil base oil from natural petroleum products, such as hydrocracking tail oil, hydrotreated wax oil, hydrorefined wax oil, and hydrorefined wax paste, etc., generally contain long-chain isomeric alkanes, long-side-chain monocyclic naphthenes, and long-chain monocyclic aromatic hydrocarbons, in addition to a certain amount of non-ideal components such as di- and polynaphthenes and aromatic hydrocarbons. These non-ideal components cannot be converted into high-viscosity-index components in the isomerization dewaxing process, and their presence severely restricts the improvement of the viscosity index of the isomerization dewaxing product-lubricating oil base oil. The inventors propose that if the non-ideal components in the feedstock can be removed in advance, without subsequent isomerization dewaxing treatment, on the one hand, the viscosity index of the isomerization dewaxing product-lubricating oil base oil can be improved, and on the other hand, the hydrogen consumption of the isomerization dewaxing process can be greatly reduced, and the operation and production costs of the device can be reduced.

[0007] Specifically, the present application mainly relates to the following aspects.

[0008] The first aspect of the present application provides a method for producing lubricating oil base oil, comprising the following steps:

[0009] (1) The feedstock is subjected to fractionation to obtain light lubricating oil and heavy lubricating oil;

[0010] (2) Under contact conditions, the light lubricating oil enters a first reaction zone and is treated with a catalyst to obtain a first stream, and the first stream is recycled back to the first reaction zone for continuous treatment;

[0011] (3) When the refractive index (20°C) of the first stream is 0.1-5% higher than that of the light lubricating oil, the light lubricating oil and the first stream stop entering the first reaction zone;

[0012] (4) Hydrogen is introduced into the first reaction zone, and the adsorbate is subjected to isomerization dewaxing reaction under the action of the catalyst and hydrogen, and the reaction product is separated to obtain No. 4 base oil and No. 6 base oil products;

[0013] (5) The heavy lubricating oil enters a second reaction zone and is treated with a catalyst to obtain a second stream, and the second stream is recycled back to the second reaction zone for continuous treatment;

[0014] (6) When the refractive index (20°C) of the second stream is 0.1-5% higher than that of the heavy lubricating oil, the heavy lubricating oil and the second stream stop entering the second reaction zone;

[0015] (7) Introduce hydrogen into the second reaction zone so that the adsorbate undergoes an isomerization dewaxing reaction under the action of catalyst and hydrogen. The reaction products are separated to obtain No. 6 base oil and No. 8 base oil products.

[0016] Furthermore, in the above-mentioned production method of lubricating oil base oil, the raw material is one or more of hydrocracking tail oil, hydrotreated wax oil, hydrotreated wax paste, and hydrotreated wax off-oil.

[0017] Furthermore, in the above-mentioned method for producing lubricating base oil, the requirements for raw material fractionation in step (1) are: the cutting temperature of light lubricating oil and heavy lubricating oil is 400-460℃, preferably 420-440℃.

[0018] Furthermore, in the above-mentioned method for producing lubricating oil base oil, the first reaction zone is equipped with one or more reactors, preferably two reactors, which are connected in parallel and switched for use. That is, when the light lubricating oil and the first material flow stop entering one reactor in the first reaction zone, the light lubricating oil is introduced into the other reactor in the first reaction zone. The reactor can be one or more of the existing fixed-bed hydrogenation reactor, fluidized-bed hydrogenation reactor, and slurry-bed hydrogenation reactor, with a fixed-bed hydrogenation reactor being preferred.

[0019] Furthermore, in the above-mentioned method for producing lubricating oil base oil, the second reaction zone is provided with one or more reactors, preferably two reactors, which are connected in parallel and used alternately. That is, when the heavy lubricating oil and the second material flow stop entering one reactor in the second reaction zone, the heavy lubricating oil is introduced into the other reactor in the second reaction zone. The reactor can be one or more of the existing fixed-bed hydrogenation reactor, fluidized-bed hydrogenation reactor, and slurry-bed hydrogenation reactor, with a fixed-bed hydrogenation reactor being preferred.

[0020] Furthermore, in the above-mentioned method for producing lubricating oil base oil, the operating conditions (adsorption reaction) of the first reaction zone in step (2) are: temperature of 40℃~250℃, preferably 60℃~200℃, pressure of 0.01MPa~0.5MPa, preferably 0.08~0.1MPa, and volume hourly space velocity of 0.05h⁻¹. -1 ~5.0h -1 Preferably 0.1h -1 ~2.0h -1 .

[0021] Furthermore, in the above-mentioned method for producing lubricating base oil, in step (3), when the refractive index (20°C) of the first material stream is 0.5 to 2.5% higher than the refractive index (20°C) of the light lubricating oil, the light lubricating oil and the first material stream are stopped from entering the first reaction zone.

[0022] Further, in the above-mentioned production method of lubricating base oil, the operating conditions (isomerization and dewaxing reaction) of the first reaction zone in step (4) are as follows: the reaction temperature is 200 to 420°C, preferably 270 to 380°C, the hydrogen partial pressure is 1.0 to 20.0 MPa, preferably 3.0 to 15.0 MPa, the volume space velocity is 0.1 to 10.0 h -1 , preferably 0.5 to 3.0 h -1 , and the hydrogen to oil volume ratio is 100:1 to 1500:1, preferably 100:1 to 400:1.

[0023] Further, in the above-mentioned production method of lubricating base oil, the separation in step (4) generally includes gas-liquid separation and fractionation. The isomerization and dewaxing reaction product is first subjected to gas-liquid separation in a gas-liquid separation zone, and after the separation, a gas phase stream and a liquid phase stream are obtained. The gas phase stream can be subjected to purification treatment and then used as recycle hydrogen to be recycled to the first reaction zone. The liquid phase stream is further subjected to separation in a fractionation column, and after the separation, No. 4 base oil and No. 6 base oil products can be obtained as needed.

[0024] Further, in the above-mentioned production method of lubricating base oil, the operating conditions (adsorption reaction) of the second reaction zone in step (5) are as follows: the temperature is 40°C to 250°C, preferably 60°C to 220°C, the pressure is 0.01 MPa to 0.5 MPa, preferably 0.08 to 0.1 MPa, the volume space velocity is 0.05 h -1 to 5.0 h -1 , preferably 0.1 h -1 to 2.0 h -1 .

[0025] Further, in the above-mentioned production method of lubricating base oil, the temperature of the adsorption reaction in the second reaction zone is higher than the temperature of the adsorption reaction in the first reaction zone by 1°C to 50°C, preferably 5°C to 30°C.

[0026] Further, in the above-mentioned production method of lubricating base oil, in step (6), when the refractive index (20°C) of the 2nd stream is higher than the refractive index (20°C) of the heavy lubricating oil feedstock by 0.5 to 2.5%, the heavy lubricating oil feedstock and the 2nd stream are stopped from being introduced into the second reaction zone.

[0027] Further, in the above-mentioned production method of lubricating base oil, the operating conditions (isomerization and dewaxing reaction) of the second reaction zone in step (7) are as follows: the reaction temperature is 200 to 420°C, preferably 290 to 400°C, the hydrogen partial pressure is 1.0 to 20.0 MPa, preferably 3.0 to 15.0 MPa, the volume space velocity is 0.1 to 10.0 h -1 , preferably 0.5 to 3.0 h -1 , and the hydrogen to oil volume ratio is 100:1 to 1500:1, preferably 200:1 to 800:1.

[0028] Further, in the production method of the lubricating oil base oil, the temperature of the isomerization and dewaxing reaction in the second reaction zone is higher than the temperature of the isomerization and dewaxing reaction in the first reaction zone by 1°C to 50°C, preferably 5°C to 30°C.

[0029] Further, in the production method of the lubricating oil base oil, the separation in step (7) generally includes gas-liquid separation and fractionation, and the isomerization and dewaxing reaction product is first subjected to gas-liquid separation in a gas-liquid separation zone, and after the separation, a gas phase stream and a liquid phase stream are obtained, and the gas phase stream can be subjected to purification treatment and then used as the recycle hydrogen to be circulated to the second reaction zone; the liquid phase stream is further subjected to separation in a fractionation column, and after the separation, a No. 6 base oil and a No. 8 base oil product can be obtained as needed.

[0030] Further, in the production method of the lubricating oil base oil, the catalysts used in the first reaction zone and the second reaction zone are the same or different.

[0031] Further, in the production method of the lubricating oil base oil, the catalyst includes an intergrowth molecular sieve of a TON structure molecular sieve and a 5A type molecular sieve, an active metal component, and an inorganic refractory oxide; preferably, the TON structure molecular sieve is intergrown on at least a part of the surface of the 5A type molecular sieve at a predetermined surface coverage, and a suitable surface coverage can be 0.5% or more or 1% or more, and 50% or less or 20% or less, but the present application is not limited thereto.

[0032] According to one embodiment of the present application, the specific surface area of the intergrowth molecular sieve is 300 m 2 / g to 600 m 2 / g, and the pore volume is 0.15 cm 3 / g to 0.40 cm 3 / g.

[0033] According to one embodiment of the present application, the specific surface area of the catalyst is 200 m 2 / g to 550 m 2 / g, and the pore volume is 0.25 cm 3 / g to 0.60 cm 3 / g.

[0034] According to one embodiment of the present application, the weight ratio of the 5A type molecular sieve to the TON structure molecular sieve is 1:80 to 3:1, preferably 1:30 to 1:1.

[0035] According to one embodiment of the present application, the content of the TON structure molecular sieve is 10wt%-80wt%, preferably 20wt%-60wt%, and the content of the 5A type molecular sieve is 1wt%-50wt%, preferably 2wt%-20wt%, relative to the total weight of the catalyst being 100wt%.

[0036] According to one embodiment of the present application, the content of the mosaic molecular sieve is 10wt%-90wt%, preferably 20wt%-70wt%, and the content of the active metal component is 0.05wt%-5.0wt%, preferably 0.1wt%-1.0wt%, relative to the total weight of the catalyst being 100wt%.

[0037] According to one embodiment of the present application, the inorganic refractory oxide is selected from one or more of alumina, titania, boria, silica, zirconia and magnesia, preferably alumina.

[0038] According to one embodiment of the present application, the active metal component is selected from at least one of the noble metals in Group VIII of the Periodic Table of Elements, preferably at least one of Pt and Pd, in particular Pt.

[0039] According to one embodiment of the present application, the TON structure molecular sieve is selected from one or more of ZSM-22, Theta-1, ISI-1, KZ-2 and NU-10, preferably ZSM-22.

[0040] According to one embodiment of the present application, the 5A type molecular sieve is selected from 5A molecular sieve.

[0041] According to one embodiment of the present application, the catalyst is prepared by kneading the mosaic molecular sieve with the inorganic refractory oxide, the extrusion aid, the binder, further forming the carrier by extrusion molding, and then loading the active metal to obtain the catalyst.

[0042] According to one embodiment of the present application, the extrusion aid and the binder can use the existing reagents commonly used in the art, and the general extrusion aid can be any one of sesbania powder and starch, and the binder is an aqueous solution of inorganic acid, which can be nitric acid solution.

[0043] According to one embodiment of the present application, the catalyst has the dual functions of adsorption and hydroisomerization, can selectively enrich long side chain hydrocarbons, and then further hydroisomerization reaction is carried out to avoid excessive isomerization phenomenon.

[0044] According to one embodiment of the present application, the preparation method of the mosaic molecular sieve comprises the following steps:

[0045] (1) contacting a silicon source, an aluminum source, and an alkali source in the presence of a template agent, a TON structure molecular sieve, and water to obtain a gel mixture, and

[0046] (2) hydrothermally crystallizing the gel mixture, and then washing, drying, and calcining to obtain a first mosaic molecular sieve.

[0047] According to one embodiment of the present application, the preparation method further comprises the following step:

[0048] (3) calcium exchanging the first mosaic molecular sieve, and then washing, drying, and calcining to obtain a second mosaic molecular sieve.

[0049] According to one embodiment of the present application, in step (1), the silicon source is selected from at least one of water glass, sodium silicate, methyl orthosilicate, ethyl orthosilicate, propyl orthosilicate, and butyl orthosilicate.

[0050] According to one embodiment of the present application, in step (1), the alkali source is selected from at least one of alkali metal hydroxides, preferably sodium hydroxide.

[0051] According to one embodiment of the present application, in step (1), the aluminum source is selected from at least one of sodium metaaluminate, aluminum isopropoxide, aluminum sulfate, aluminum hydroxide, aluminum oxide, and pseudo-boehmite.

[0052] According to one embodiment of the present application, in step (1), the template agent is selected from at least one of polyethylene oxide tri-block copolymer (P123) and dimethyloctadecyl [3- (trimethoxysilyl) propyl] ammonium chloride (TPOAC).

[0053] According to one embodiment of the present application, in step (1), the TON structure molecular sieve is selected from one or more of ZSM-22, Theta-1, ISI-1, KZ-2, and NU-10, preferably ZSM-22.

[0054] According to one embodiment of the present application, in step (1), the operation conditions of the contacting include: under stirring, the temperature is 15-30℃, and the time is 1-4h.

[0055] According to one embodiment of the present application, in step (1), the molar ratio of the alkali source (calculated as an oxide), the silicon source (calculated as SiO2), the aluminum source (calculated as Al2O3), the template agent, and water is (0.5-2.5):1:(0.4-0.7):(0.001-0.08):(30-200), and the amount of the TON structure molecular sieve is 0.3-8 times, preferably 1-7 times, of the amount of the silicon source.

[0056] According to one embodiment of the present application, in step (2), the hydrothermal crystallization temperature is 60-120℃, and the crystallization time is 2-16h.

[0057] According to one embodiment of the present application, in step (2), the drying temperature is 80-200℃, and the drying time is 2-24h.

[0058] According to one embodiment of the present application, in step (2), the calcination temperature is 400-600℃, and the calcination time is 2-12h.

[0059] According to one embodiment of the present application, in step (3), the operation conditions of the calcium exchange include: the exchange temperature is 60-100℃, the exchange time is 1-12h, and the calcium ion concentration in the calcium exchange solution is 0.1-2.5mol / L.

[0060] According to one embodiment of the present application, in step (3), the drying temperature is 80-150℃, and the drying time is 2-12h.

[0061] According to one embodiment of the present application, in step (3), the calcination temperature is 300-500℃, and the calcination time is 2-8h.

[0062] The second aspect of the present application provides a production system of lubricating oil base oil, comprising:

[0063] a fractionation unit for receiving raw material, and obtaining light lubricating oil material and heavy lubricating oil material after fractionation;

[0064] a first reaction zone for receiving the light lubricating oil material from the fractionation unit, and performing adsorption reaction on the light lubricating oil material with the catalyst filled in the first reaction zone, and obtaining the first stream after adsorption treatment, and recycling the first stream back to the first reaction zone for treatment, and stopping the light lubricating oil material and the first stream from entering the first reaction zone when the refractive index (20℃) of the first stream is higher than the refractive index (20℃) of the light lubricating oil material by 0.1-5%, preferably by 0.5-2.5%, and introducing hydrogen into the first reaction zone, and performing isomerization and condensation reaction under the action of the catalyst and the hydrogen;

[0065] a first separation unit comprising a gas-liquid separation zone and a fractionation tower, and being used for receiving the reaction product from the first reaction zone, and obtaining the No. 4 base oil and the No. 6 base oil product after separation;

[0066] a second reaction zone for receiving the heavy lubricating oil, the heavy lubricating oil is contacted with catalysts packed in the second reaction zone to perform adsorption reaction, the second stream obtained after adsorption treatment is recycled back to the second reaction zone for treatment, when the refractive index (20℃) of the second stream is 0.1-5%, preferably 0.5-2.5% higher than the refractive index (20℃) of the heavy lubricating oil, the heavy lubricating oil and the second stream stop entering the second reaction zone, and hydrogen is introduced into the second reaction zone, and isomerization and condensation reduction reaction occurs under the action of the catalysts and the hydrogen;

[0067] a second separation unit comprising a gas-liquid separation zone and a fractionating column, which is used for receiving the reaction product from the second reaction zone, and 6# base oil and 8# base oil products are obtained after separation.

[0068] Further, in the above lubricating base oil production system, the first reaction zone is provided with one or more reactors, preferably two reactors, which are connected in parallel and used alternately, i.e., when the light lubricating oil and the first stream stop entering one of the reactors in the first reaction zone, the light lubricating oil enters the other reactor in the first reaction zone; the reactors can be one or more of the existing fixed bed hydrogenation reactor, fluidized bed hydrogenation reactor and slurry bed hydrogenation reactor, and preferably a fixed bed hydrogenation reactor.

[0069] Further, in the above lubricating base oil production system, the second reaction zone is provided with one or more reactors, preferably two reactors, which are connected in parallel and used alternately, i.e., when the heavy lubricating oil and the second stream stop entering one of the reactors in the second reaction zone, the heavy lubricating oil enters the other reactor in the second reaction zone; the reactors can be one or more of the existing fixed bed hydrogenation reactor, fluidized bed hydrogenation reactor and slurry bed hydrogenation reactor, and preferably a fixed bed hydrogenation reactor.

[0070] Further, in the above lubricating base oil production system, the gas-liquid separation zone can adopt any one of the existing devices that can realize gas-liquid two-phase separation function in the art, such as a gas-liquid separator, a flash column, etc. The gas-liquid separation zone is used for receiving the isomerization and condensation reduction reaction product from the first reaction zone or the second reaction zone, and after separation, a gas phase stream and a liquid phase stream are obtained; the gas phase stream obtained after separation is purified and then communicated with the first reaction zone or the second reaction zone through a pipeline, and is used as recycled hydrogen; the liquid phase stream enters the fractionating column, and is separated according to the required target product, and different viscosity lubricating base oil products are obtained after fractionation.

[0071] Compared with the prior art, the production method and production system of the lubricating base oil provided by the application have the following advantages:

[0072] 1. The high viscosity index lubricating oil base oil production method provided by the application adopts a segmented feeding mode, first fractionates the raw material, and makes the light lubricating oil material and the heavy lubricating oil material react under suitable conditions respectively, solves the problem that the pour point and the viscosity index of the product cannot be considered, avoids excessive isomerization of lighter components, improves the viscosity index and yield of the base oil product, and can simultaneously produce No. 4, No. 6 and No. 8 base oil products meeting the requirements of API Class III.

[0073] 2. In the lubricating oil base oil production method provided by the application, non-ideal components are separated out by pre-adsorbing the raw material, so that only the raw material rich in ideal components such as long-chain isomeric alkanes, long-side-chain monocyclic naphthenes and long-chain monocyclic aromatics is subjected to isomerization pour point depression reaction, thereby realizing the generation of high viscosity index lubricating oil base oil products, greatly reducing the participation of non-ideal components in hydrogenation reaction, reducing the isomerization pour point depression process load and hydrogen consumption, and improving the economic efficiency of the device. Moreover, the applicant found in the research process that the addition of 5A molecular sieve to the currently used hydroisomerization dewaxing catalyst has selective adsorption effect on the raw material of the lubricating oil base oil in the absence of hydrogen, which can separate the non-ideal components such as two-ring or more ring naphthenes and part of aromatics with low viscosity index in the raw material, thereby reducing the content of low viscosity index components in the lubricating oil base oil product from the raw material aspect and improving the viscosity index of the lubricating oil base oil product.

[0074] 3. In the lubricating oil base oil production method provided by the application, the catalyst has selective adsorption ability to long-chain isomeric alkanes, long-side-chain monocyclic naphthenes and long-chain monocyclic aromatics, and selective isomerization ability to alkanes in the presence of hydrogen and under suitable reaction conditions, which simplifies the production process of the lubricating oil base oil, reduces the investment of the device and reduces the hydrogen consumption of the process.

[0075] 4. In the lubricating oil base oil production method provided by the application, the adsorption separation efficiency is characterized by the change of the refractive index of the raw material before and after adsorption treatment. This parameter is simple and convenient to measure and can directly reflect the separation effect of the ideal components rich in long-chain isomeric alkanes, long-side-chain monocyclic naphthenes and long-chain monocyclic aromatics in the raw material.

[0076] 5. The molecular sieve in the catalyst provided by the application is combined by 5A molecular sieve and TON structure molecular sieve in a mutual inlaying mode. The 5A molecular sieve has good adsorption function and can enrich alkanes. The TON structure molecular sieve has specific pore structure and suitable acidity and is conducive to the selective isomerization of alkanes. The molecular sieve composition provided by the application has the above specific functions and still maintains good adsorption performance after being loaded with active metals. After the catalyst prepared by using the molecular sieve composition provided by the application as a component is subjected to isomerization reaction and regeneration, the molecular sieve still maintains good stability. Attached Figure Description

[0077] Figure 1 This is a schematic diagram of the production process of the lubricating oil base oil of the present invention. Detailed Implementation

[0078] The present invention will now be described in further detail with reference to the accompanying drawings and specific embodiments. The following embodiments will further illustrate the method provided by the present invention, but do not limit the scope of the invention.

[0079] Unless otherwise expressly stated, throughout the specification and claims, the term "comprising" or its variations such as "including" or "comprises" shall be understood to include the stated elements or components without excluding other elements or other components.

[0080] In this document, for ease of description, spatial relative terms such as “below,” “under,” “down,” “above,” “above,” “up,” etc., are used to describe the relationship of one element or feature to another element or feature in the accompanying drawings. It should be understood that spatial relative terms are intended to encompass different orientations of an object in use or operation, in addition to those depicted in the figures. For example, if an object in the figure is flipped, an element described as “below” or “under” another element or feature would be oriented “above” that element or feature. Thus, the exemplary term “below” can encompass both the downward and upward orientations. An object may also have other orientations (rotated 90 degrees or other orientations), and the spatial relative terms used herein should be interpreted accordingly.

[0081] In this document, the terms "first," "second," etc., are used to distinguish two different elements or parts, and are not used to define specific positions or relative relationships. In other words, in some embodiments, the terms "first," "second," etc., can also be used interchangeably.

[0082] In this document, all numeric values ​​of parameters (e.g., quantity or condition) should be understood to be modified by the term “about” in all cases, regardless of whether “about” actually appears before the numeric value.

[0083] In the context of this specification, unless explicitly stated otherwise, both the silicon-aluminum material and the catalyst undergo calcination treatment, sometimes referred to as "calcination form," prior to measurement. The conditions for this calcination treatment include: calcination at 600°C in an air atmosphere for a calcination time of 3 hours or more.

[0084] In the context of the present specification, long side chain hydrocarbon particularly refers to one or several of long side chain isohydrocarbon, long side chain monocyclic naphthene and long side chain monocyclic aromatic hydrocarbon, excluding other hydrocarbons with long side chain. In addition, according to the present application, long side chain refers to C8-22 (preferably C10-18) straight chain alkyl as side chain.

[0085] In the context of the present specification, mechanical mixture refers to a mixture of two or more materials obtained by mechanical mixing. Here, the mechanical mixing includes simple mixing, grinding, pulping, etc.

[0086] In the context of the present specification, mosaic molecular sieve refers to one or more molecular sieve crystals with the surface or interior of another one or more molecular sieves inlaid, which is a composite crystal with two or more molecular sieve structural characteristics. Compared with mechanical mixture, the combination of different molecular sieves in mosaic structure is more compact, and a truly integrated composite structure at molecular level is formed.

[0087] In the context of the present specification, refractive index is characterized by Mettler refractometer R5, long chain hydrocarbon content is characterized by Agilent gas chromatograph 7890, XRD pattern of sample is characterized by D / max-2500 full-automatic rotating target X-ray diffractometer, specific surface area, pore volume and average pore diameter of mosaic molecular sieve and specific surface area, pore volume and average pore diameter of catalyst are tested and characterized by N2 adsorption-desorption method using ASAP 2405 physical adsorption instrument, calcium content of calcium type molecular sieve is characterized by X-ray fluorescence diffraction.

[0088] In the context of the present specification, the content of TON structure molecular sieve in mosaic molecular sieve is quantitatively analyzed by XRD determination.

[0089] In the absence of explicit indication, all percentages, parts, ratios, etc. mentioned in the present specification are based on weight, pressure is gauge pressure, and weight or content is on a dry basis.

[0090] As Figure 1As shown, the lubricating oil base oil production method of the first embodiment of the present application, the raw material 1 enters the fractionation unit 2 after fractionation to obtain light lubricating oil material 3 and heavy lubricating oil material 4, wherein the light lubricating oil material 3 enters the first reaction zone 5, and after being treated by contacting with the catalyst, the first stream 6 is obtained, and the first stream 6 is recycled back to the first reaction zone 5 for continuous treatment; when the refractive index (20℃) of the first stream 6 is 0.1-5% higher than that of the light lubricating oil material, the light lubricating oil material 3 and the first stream 6 stop entering the first reaction zone 5; hydrogen 23 is introduced into the first reaction zone 5, so that the adsorbent is subjected to isomerization and condensation reaction under the action of the catalyst and hydrogen, and the reaction product 7 enters the first separation unit, which includes the first gas-liquid separation zone 8 and the first fractionation column 13; after the reaction product 7 is separated in the first gas-liquid separation zone 8, the gas phase material 9 and the liquid phase material 10 are obtained, and the liquid phase material 10 enters the first fractionation column 13 to obtain the No. 4 base oil product 11 and the No. 6 base oil product 12 after separation. The heavy lubricating oil material 4 enters the second reaction zone 14, and after being treated by contacting with the catalyst, the second stream 15 is obtained, and the second stream 15 is recycled back to the second reaction zone 14 for continuous treatment; when the refractive index (20℃) of the second stream 15 is 0.1-5% higher than that of the heavy lubricating oil material, the heavy lubricating oil material 4 and the second stream 15 stop entering the second reaction zone 14; hydrogen 24 is introduced into the second reaction zone 14, so that the adsorbent is subjected to isomerization and condensation reaction under the action of the catalyst and hydrogen, and the reaction product 16 enters the second separation unit, which includes the second gas-liquid separation zone 17 and the second fractionation column 22; after the reaction product 16 is separated in the second gas-liquid separation zone 17, the gas phase material 18 and the liquid phase material 19 are obtained, and the liquid phase material 19 enters the second fractionation column 22 to obtain the No. 6 lubricating oil base oil product 20 and the No. 8 base oil product 21 after separation.

[0091] The raw material oil used in the method embodiments and the comparative examples of the present application includes four kinds of hydrocracking tail oil, hydrocracked wax oil, hydrocracked wax paste and hydrocracked wax foot oil. The specific properties of the raw material oil are shown in Table 1.

[0092] Table 1 Properties of raw material oil

[0093]

[0094] Example 1

[0095] A crystallization kettle was charged with 128 g of sodium hydroxide, 208 g of tetraethyl orthosilicate, 82 g of sodium metaaluminate, 14.88 g of dimethyloctadecyl[3-(trimethoxysilyl)propyl]ammonium chloride (TPOAC), and 1800 g of water, and the mixture was stirred to homogeneity. Then, 300 g of ZSM-22 zeolite was added to the mixture, and the resulting mixture was stirred. The crystallization kettle was sealed, and the temperature was increased to 110°C. The mixture was hydrothermally crystallized at 110°C for 6 h. After the crystallization was completed, the product was washed, and then dried at 110°C for 6 h. The dried product was calcined at 500°C for 5 h to obtain a first embedded zeolite Z2. The embedded zeolite Z2 was ion-exchanged in a 1.8 mol / L CaCl2 solution at 90°C for 4 h. The product was filtered, washed, and then dried at 100°C for 4 h. The dried product was calcined at 400°C for 3 h to obtain a second embedded zeolite GZ-1. The specific surface area of the second embedded zeolite GZ-1 was 452 m2 / g, the pore volume was 0.25 mL / g, and the mass fraction of TON structure zeolite was 85%. 2 / g, the pore volume was 0.25 mL / g, and the mass fraction of TON structure zeolite was 85%.

[0096] The second embedded zeolite GZ-1 was mixed with 90 g of pseudoboehmite (dry basis) and 20 g of sesbania powder to obtain a mixture. The mixture was kneaded with 9 ml of concentrated nitric acid (65% by mass) and an appropriate amount of water. The kneaded mixture was extruded into a strip shape. The extruded support was dried at 100°C for 4 h and then calcined at 550°C for 4 h to obtain a support ES-1. The support ES-1 was impregnated with a noble metal Pt by a saturation impregnation method. The Pt loading amount was 0.50% by mass of the support. The impregnated support was dried at 100°C for 6 h and then calcined at 500°C for 3 h to obtain a catalyst of the present application, which was designated as CAT-1.

[0097] Example 2

[0098] A crystallization kettle was charged with 200 g of sodium hydroxide, 208 g of tetraethyl orthosilicate, 98.4 g of sodium metaaluminate, 39.68 g of dimethyloctadecyl[3-(trimethoxysilyl)propyl]ammonium chloride (TPOAC), and 3600 g of water, and the mixture was stirred to homogeneity. Then, 420 g of ZSM-22 zeolite was added to the mixture, and the resulting mixture was stirred. The crystallization kettle was sealed, and the temperature was increased to 100°C. The mixture was hydrothermally crystallized at 100°C for 8 h. After the crystallization was completed, the product was washed, and then dried at 100°C for 8 h. The dried product was calcined at 500°C for 3 h to obtain a first embedded zeolite Z2. The embedded zeolite Z2 was ion-exchanged in a 2.1 mol / L CaCl2 solution at 100°C for 2 h. The product was filtered, washed, and then dried at 100°C for 3 h. The dried product was calcined at 500°C for 3 h to obtain a second embedded zeolite GZ2. The specific surface area of the second embedded zeolite GZ2 was 387 m2 / g, the pore volume was 0.33 mL / g, and the mass fraction of TON structure zeolite was 89%.

[0099] The catalyst of the present application is prepared according to the process of Example 1, except that the mosaic molecular sieve used is GZ2, and the Pt loading is 0.47wt% of the support. The catalyst of the present application prepared is designated as CAT-2.

[0100] Example 3

[0101] A crystallization kettle is charged with 80g of sodium hydroxide, 184g of sodium silicate, 65.6g of sodium metaaluminate, 4.96g of dimethyloctadecyl[3-(trimethoxysilyl)propyl]ammonium chloride (TPOAC), and 540g of water, and stirred to obtain a uniform mixture. Then, 42g of ZSM-22 molecular sieve is added and stirred, and the reaction kettle is sealed, heated to 120℃, and hydrothermally crystallized for 5h. After crystallization, the product obtained is washed, dried at 120℃ for 5h, and then calcined at 500℃ for 4h, thereby obtaining a first mosaic molecular sieve Z3. Then, the molecular sieve Z3 is ion-exchanged in a 1.2mol / L CaCl2 solution at 70℃ for 6h, filtered and washed, dried at 100℃ for 4h, and then calcined at 450℃ for 3h, thereby obtaining a second mosaic molecular sieve GZ-3, which has a specific surface area of 573m2 / g, a pore volume of 0.19mL / g, and a TON structure molecular sieve mass fraction of 47%.

[0102] The catalyst 3 of the present application is prepared according to the process of Example 1, except that the mosaic molecular sieve used is GZ-3, and the Pt loading is 0.31wt% of the support. The catalyst of the present application prepared is designated as CAT-3.

[0103] Example 4

[0104] Example 4 uses the hydrocracking tail oil listed in Table 1 as the raw material, and uses the process flow described, and the catalyst CAT-1 is used in the first reaction zone and the second reaction zone. The process conditions are shown in Table 2, and the results are shown in Table 3. Figure 1 The catalyst 3 of the present application is prepared according to the process of Example 1, except that the mosaic molecular sieve used is GZ-3, and the Pt loading is 0.31wt% of the support. The catalyst of the present application prepared is designated as CAT-3.

[0105] Example 5

[0106] Example 5 uses the hydrocracking tail oil listed in Table 1 as the raw material, and uses the process flow described, and the catalyst CAT-2 is used in the first reaction zone and the second reaction zone. The process conditions are shown in Table 2, and the results are shown in Table 3. Figure 1 The catalyst 3 of the present application is prepared according to the process of Example 1, except that the mosaic molecular sieve used is GZ-3, and the Pt loading is 0.31wt% of the support. The catalyst of the present application prepared is designated as CAT-3.

[0107] Example 6

[0108] Example 4 uses the hydrocracking tail oil listed in Table 1 as the raw material, and uses the process flow described, and the catalyst CAT-3 is used in the first reaction zone and the second reaction zone. The process conditions are shown in Table 2, and the results are shown in Table 3. Figure 1 The catalyst 3 of the present application is prepared according to the process of Example 1, except that the mosaic molecular sieve used is GZ-3, and the Pt loading is 0.31wt% of the support. The catalyst of the present application prepared is designated as CAT-3.

[0109] Comparative Example 1

[0110] ZSM-22 molecular sieve (Si / Al ratio 90) 134 g, 5A molecular sieve 200 g and 150 g (in terms of alumina) aluminum hydroxide (SB produced by Condean Company, Germany), 30 g of sesbania powder were mixed uniformly, then water and concentrated nitric acid (mass concentration 66.5 wt%) were added, and they were kneaded sufficiently to become a paste-like plastic material, which was extruded into cylindrical strips with a diameter of 1.5 mm on an extruder. The cylindrical strips were dried at 100 ℃ for 12 hours, and then calcined at 550 ℃ in an air atmosphere for 4 hours to obtain the catalyst carrier of the present application.

[0111] 300 g of the carrier was loaded with noble metal Pt by saturated impregnation, then dried at 110 ℃ for 7 hours, and calcined at 500 ℃ in an air atmosphere for 3 h to prepare the catalyst of the present application containing 0.49 wt% Pt, numbered C-D1.

[0112] Comparative Example 2

[0113] 40 g of sodium hydroxide, 208 g of tetraethyl orthosilicate, 285.6 g of aluminum isopropoxide, 5.75 g of polyethylene oxide triblock copolymer (P123), and 1440 g of water were mixed uniformly and loaded into a crystallization kettle, then 60 g of Hβ molecular sieve was added and stirred, then the reaction kettle was sealed, heated to 90 ℃, and hydrothermally crystallized for 10 h. After the crystallization was completed, the product obtained by crystallization was washed, then dried at 110 ℃ for 6 h, and then placed in a muffle furnace at 450 ℃ for 8 h to obtain a first mosaic molecular sieve. Then the molecular sieve was ion exchanged in a 1.8 mol / L CaCl2 solution at 90 ℃ for 4 h, suction filtered and washed, then dried at 100 ℃ for 4 h, and then placed in a muffle furnace at 400 ℃ for 3 h to obtain a second mosaic molecular sieve D.

[0114] The preparation process of the comparative catalyst C-D2 of the present application is the same as that of Example 1, except that the mosaic molecular sieve D is used, and the Pt loading is 0.30 wt% of the carrier. The prepared catalyst is numbered C-D2.

[0115] Comparative Example 3: Comparative Example 3 used the hydrocracking tail oil listed in Table 1 as the raw material, and used the process flow described above, and both the first reaction zone and the second reaction zone used catalyst C-D1. The process conditions are shown in Table 2, and the results are shown in Table 3. Figure 1

[0116] Comparative Example 4

[0117] Comparative Example 4 used the hydrocracking tail oil listed in Table 1 as the raw material, and used the process flow described above, and both the first reaction zone and the second reaction zone used catalyst C-D2. The process conditions are shown in Table 2, and the results are shown in Table 3. Figure 1

[0118] ​​Table 2 Process conditions for Examples 4-6 and Comparative Examples 3-4

[0119] Example No. Example 4 Example 5 Example 6 Comparative Example 3 Comparative Example 4 Adsorption process conditions for the first reaction zone Adsorption temperature / °C 200 160 120 200 160 Adsorption pressure / MPa 0.08 0.09 0.10 0.08 0.09 Volume space velocity / h -1 ]] 0.5 1.0 1.5 0.5 1.0 Refractive index of the 1st stream (20°C) 1.493 1.491 1.484 1.480 1.4900 Adsorption process conditions for the second reaction zone Adsorption temperature / °C 220 170 140 220 170 Adsorption pressure / MPa 0.08 0.09 0.10 0.08 0.09 Volume space velocity / h -1 ]] 0.5 1.0 1.5 0.5 1.0 Refractive index of the 2nd stream (20°C) 1.501 1.498 1.493 1.490 1.497 Isomerization process conditions for the first reaction zone Reaction temperature / °C 360 320 280 360 320 Reaction pressure / MPa 8.0 10.0 14.0 8.0 10.0 Volume ratio of hydrogen to oil 400 300 200 400 300 Volume space velocity / h -1 ]] 1.0 2.0 3.0 1.0 2.0 Isomerization process conditions for the second reaction zone Reaction temperature / °C 380 340 300 380 340 Reaction pressure / MPa 8.0 10.0 14.0 8.0 10.0 Volume ratio of hydrogen to oil 400 300 200 400 300 Volume space velocity / h -1 ]] 1.0 2.0 3.0 1.0 2.0

[0120] Table 3 Product properties for Examples 4-6 and Comparative Examples 3-4

[0121] Example No. Example 4 Example 5 Example 6 Comparative Example 3 Comparative Example 4 No. 2 base oil (first reaction zone) Pour point / °C -32 -24 -21 -15 -12 Viscosity (100°C), mm / s 2 ]] 2.10 2.09 2.12 2.07 2.11 Viscosity index 106 101 99 97 94 No. 4 base oil (first reaction zone) Pour point / °C -24 -21 -18 -9 -6 Viscosity (100°C), mm / s 2 ]]> 4.19 4.15 4.20 4.06 4.17 Viscosity index 121 117 115 108 104 No. 6 base oil (second reaction zone) Pour point / °C -21 -15 -12 -6 -3 Viscosity (100°C), mm / s 2 ]]> 5.98 5.93 6.02 5.96 6.07 Viscosity index 125 122 121 110 107 No. 8 base oil (second reaction zone) Pour point / °C -15 -9 -6 -3 0 Viscosity (100°C), mm / s 2 ]] 7.79 7.84 7.80 7.75 7.81 Viscosity index 131 127 124 116 114

Claims

1. A method for producing a lubricating oil base oil, comprising the steps of: (1) obtaining a light lubricating oil material and a heavy lubricating oil material by fractionating a feedstock; the feedstock being one or more of a hydrocracking tail oil, a hydrocracked gas oil, a hydrocracked wax, and a hydrocracked foots oil; (3) stopping the light lubricating oil material and the first stream from entering the first reaction zone when the refractive index at 20°C of the first stream is 0.1 to 5% higher than the refractive index at 20°C of the light lubricating oil material; (4) introducing hydrogen into the first reaction zone, and causing the adsorbate to undergo an isomerization and a pour point depression reaction in the presence of a catalyst and the hydrogen, and separating the reaction product to obtain a No. 4 base oil and a No. 6 base oil product; (6) stopping the heavy lubricating oil material and the second stream from entering the second reaction zone when the refractive index at 20°C of the second stream is 0.1 to 5% higher than the refractive index at 20°C of the heavy lubricating oil material; (7) introducing hydrogen into the second reaction zone, and causing the adsorbate to undergo an isomerization and a pour point depression reaction in the presence of a catalyst and the hydrogen, and separating the reaction product to obtain a No. 6 base oil and a No. 8 base oil product; the temperature of the adsorption reaction in the second reaction zone being 1°C to 50°C higher than the temperature of the adsorption reaction in the first reaction zone; and the temperature of the isomerization and pour point depression reaction in the second reaction zone being 1°C to 50°C higher than the temperature of the isomerization and pour point depression reaction in the first reaction zone; the catalyst comprising a mosaic molecular sieve of a TON structure molecular sieve and a 5A molecular sieve, an active metal component, and an inorganic refractory oxide; the active metal component being at least one selected from the group consisting of Group VIII noble metals of the periodic table. The cut temperature of the light lubricating oil material and the heavy lubricating oil material in step (1) is 400 to 460°C. (2) under the contacting condition, the light lubricating oil enters the first reaction zone, and after being treated by the catalyst, a first stream is obtained, the first stream is recycled back to the first reaction zone for continuous treatment; the operating conditions of the first reaction zone adsorption reaction are as follows: the temperature is 40°C-250°C, the pressure is 0.01 MPa-0.5 MPa, the volume space velocity is 0.05 h -1 -5.0 h -1 ; The cut temperature of the light lubricating oil material and the heavy lubricating oil material in step (1) is 420 to 440°C. The first reaction zone is provided with one or more reactors. (5) The heavy lubricating oil enters the second reaction zone, is treated with the catalyst to obtain a second stream, and the second stream is recycled back to the second reaction zone for continuous treatment; the operating conditions of the adsorption reaction in the second reaction zone are as follows: the temperature is 40-250°C, the pressure is 0.01-0.5 MPa, the volume space velocity is 0.05-5.0 h -1 -1 -1 ; The first reaction zone is provided with two reactors, which are connected in parallel and used alternately, i.e., when the light lubricating oil material and the first stream are stopped from entering one of the reactors in the first reaction zone, the light lubricating oil material is introduced into the other reactor in the first reaction zone. The second reaction zone is provided with one or more reactors. The second reaction zone is provided with two reactors, which are connected in parallel and used alternately, i.e., when the heavy lubricating oil material and the second stream are stopped from entering one of the reactors in the second reaction zone, the heavy lubricating oil material is introduced into the other reactor in the second reaction zone. In step (3), the light lubricating oil material and the first stream are stopped from entering the first reaction zone when the refractive index at 20°C of the first stream is 0.5 to 2.5% higher than the refractive index at 20°C of the light lubricating oil material.

2. The production process of lubricating oil base oil according to claim 1, characterized by: The temperature of the adsorption reaction in the second reaction zone is 5°C to 30°C higher than the temperature of the adsorption reaction in the first reaction zone.

3. The production process of lubricating oil base oil according to claim 1, characterized by: In step (6), the heavy lubricating oil material and the second stream are stopped from entering the second reaction zone when the refractive index at 20°C of the second stream is 0.5 to 2.5% higher than the refractive index at 20°C of the heavy lubricating oil material.

4. The production process of lubricating oil base oil according to claim 1, characterized by: The temperature of the isomerization and pour point depression reaction in the second reaction zone is 5°C to 30°C higher than the temperature of the isomerization and pour point depression reaction in the first reaction zone.

5. The process for producing a lubricating oil base oil according to claim 1, characterized by: The TON structure molecular sieve is mosaic-embedded on at least a part of the surface of the 5A molecular sieve at a predetermined surface coverage, and a suitable surface coverage is 0.5% or more and 50% or less.

6. The process for producing a lubricating oil base oil according to claim 1, characterized by: ​ 7. The process for producing a lubricating oil base oil according to claim 1, characterized by: ​ 8. The process for producing a lubricating oil base oil according to claim 1, characterized by: The operating conditions of the adsorption reaction in the first reaction zone in step (2) are as follows: temperature 60-200°C, pressure 0.08-0.1 MPa, volume space velocity 0.1-2.0 h -1 -1 -1 .

9. The process for producing a lubricating oil base oil according to claim 1, characterized by: ​ 10. The process for producing a lubricating oil base oil according to claim 1, characterized by: The operating conditions of the isomerization and dewaxing reaction in the first reaction zone in step (4) are as follows: reaction temperature 200-420°C, hydrogen partial pressure 1.0-20.0 MPa, volume space velocity 0.1-10.0 h -1 -1, and hydrogen to oil volume ratio 100:1-1500:

1.

11. The process for producing a lubricating oil base oil according to claim 1, characterized by: The operating conditions of the isomerization and dewaxing reaction in the first reaction zone in step (4) are as follows: reaction temperature 270-380°C, hydrogen partial pressure 3.0-15.0 MPa, volume space velocity 0.5-3.0 h -1 -1, and hydrogen to oil volume ratio 100:1-400:

1.

12. The process for producing a lubricating oil base oil according to claim 1, characterized by: The operating conditions of the adsorption reaction in the second reaction zone in step (5) are as follows: temperature 60-220°C, pressure 0.08-0.1 MPa, volume space velocity 0.1-2.0 h -1 -1 -1 .

13. The process for producing a lubricating oil base oil according to claim 1, characterized by: ​ 14. The process for producing a lubricating oil base oil according to claim 1, characterized by: ​ 15. The process for producing a lubricating oil base oil according to claim 1, characterized by: The operating conditions of the isomerization and condensation reaction in the second reaction zone in step (7) are as follows: reaction temperature 200-420℃, hydrogen partial pressure 1.0-20.0 MPa, volume space velocity 0.1-10.0 h -1 -1, and hydrogen to oil volume ratio 100:1-1500:

1.

16. The process for producing a lubricating oil base oil according to claim 1, characterized by: The operating conditions of the isomerization and condensation reaction in the second reaction zone in step (7) are as follows: reaction temperature 290-400°C, hydrogen partial pressure 3.0-15.0 MPa, volume space velocity 0.5-3.0 h -1 -1, and hydrogen to oil volume ratio 200:1-800:

1.

17. The process for producing a lubricating oil base oil according to claim 1, characterized by: ​ 18. The process for producing a lubricating oil base oil according to claim 1, characterized by: ​ 19. The process for producing a lubricating oil base oil according to claim 1, characterized by: The TON structure molecular sieve is inlaid on at least a part of the surface of the 5A type molecular sieve with a predetermined surface coverage, and a suitable surface coverage is 0.5% or more and 20% or less.

20. The process for producing a lubricating oil base oil according to claim 1, characterized by: The TON structure molecular sieve is inlaid on at least a part of the surface of the 5A type molecular sieve with a predetermined surface coverage, and a suitable surface coverage is 1% or more and 50% or less.

21. The process for producing a lubricating oil base oil according to claim 1, characterized by: The TON structure molecular sieve is inlaid on at least a part of the surface of the 5A type molecular sieve with a predetermined surface coverage, and a suitable surface coverage is 1% or more and 20% or less.

22. The process for producing a lubricating oil base oil according to claim 1, characterized by: The weight ratio of the 5A type molecular sieve to the TON structure molecular sieve is 1:80-3:

1.

23. The process for producing a lubricating oil base oil according to claim 1, characterized by: The weight ratio of the 5A type molecular sieve to the TON structure molecular sieve is 1:30-1:

1.

24. The process for producing a lubricating oil base oil according to claim 1, characterized by: The content of the inlaid molecular sieve is 10wt%-90wt% and the content of the active metal component is 0.05wt%-5.0wt% in terms of metal elements, based on 100wt% of the total weight of the catalyst.

25. The process for producing a lubricating oil base oil according to claim 1, characterized by: The content of the inlaid molecular sieve is 20wt%-70wt% and the content of the active metal component is 0.1wt%-1.0wt% in terms of metal elements, based on 100wt% of the total weight of the catalyst.

26. The process for producing a lubricating oil base oil according to claim 1, characterized by: The inorganic refractory oxide is selected from one or more of alumina, titania, boria, silica, zirconia and magnesia.

27. The process for producing a lubricating oil base oil according to claim 1, characterized by: The inorganic refractory oxide is alumina.

28. The process for producing a lubricating oil base oil according to claim 1, characterized by: The active metal component is selected from at least one of Pt and Pd.

29. The process for producing a lubricating oil base oil according to claim 1, characterized by: The active metal component is Pt.

30. The process for producing a lubricating oil base oil according to claim 1, characterized by: The TON structure molecular sieve is selected from one or more of ZSM-22, Theta-1, ISI-1, KZ-2 and NU-10; and the 5A type molecular sieve is selected from 5A molecular sieve.

31. The process for producing a lubricating oil base oil according to claim 1, characterized by: The TON structure molecular sieve is selected from ZSM-22; and the 5A type molecular sieve is selected from 5A molecular sieve.

32. A production system for carrying out the production method of the lubricating oil base oil according to any one of claims 1-31, comprising: a fractionation unit for receiving a raw material, the raw material being fractionated to obtain a light lubricating oil material and a heavy lubricating oil material; a first reaction zone for receiving the light lubricating oil material from the fractionation unit, the light lubricating oil material being subjected to an adsorption reaction with a catalyst packed in the first reaction zone, and a first stream obtained after the adsorption treatment being circulated back to the first reaction zone for treatment, and the light lubricating oil material and the first stream being stopped from entering the first reaction zone when the 20°C refractive index of the first stream is 0.1-5% higher than that of the light lubricating oil material, and hydrogen gas being introduced into the first reaction zone to cause an isomerization and a condensation reduction reaction under the action of the catalyst and the hydrogen gas; a first separation unit including a gas-liquid separation zone and a fractionation column for receiving a reaction product from the first reaction zone, and obtaining a No. 4 base oil and a No. 6 base oil product after the separation; and a second reaction zone for receiving the No. 4 base oil from the first separation unit, the No. 4 base oil being subjected to an adsorption reaction with a catalyst packed in the second reaction zone, and a second stream obtained after the adsorption treatment being circulated back to the second reaction zone for treatment, and the No. 4 base oil and the second stream being stopped from entering the second reaction zone when the 20°C refractive index of the second stream is 0.1-5% higher than that of the No. 4 base oil, and hydrogen gas being introduced into the second reaction zone to cause an isomerization and a condensation reduction reaction under the action of the catalyst and the hydrogen gas. The second reaction zone is used for receiving the heavy lubricating oil, the heavy lubricating oil is contacted with the catalyst filled in the second reaction zone to carry out the adsorption reaction, the second stream obtained after the adsorption treatment is circulated back to the second reaction zone for treatment, when the 20℃ refractive index of the second stream is 0.1-5% higher than that of the heavy lubricating oil, the heavy lubricating oil and the second stream stop entering the second reaction zone, and hydrogen is introduced into the second reaction zone, and the isomerization and condensation reduction reaction occurs under the action of the catalyst and the hydrogen. The second separation unit comprises a gas-liquid separation zone and a fractionating column, and is used for receiving the reaction product from the second reaction zone, and the 6# base oil and the 8# base oil product are obtained after the separation.

33. The production system of claim 32, wherein: When the 20℃ refractive index of the first stream is 0.5-2.5% higher than that of the light lubricating oil, the light lubricating oil and the first stream stop entering the first reaction zone, and hydrogen is introduced into the first reaction zone, and the isomerization and condensation reduction reaction occurs under the action of the catalyst and the hydrogen.

34. The production system of claim 32, wherein: When the 20℃ refractive index of the second stream is 0.5-2.5% higher than that of the heavy lubricating oil, the heavy lubricating oil and the second stream stop entering the second reaction zone, and hydrogen is introduced into the second reaction zone, and the isomerization and condensation reduction reaction occurs under the action of the catalyst and the hydrogen.

35. The production system of claim 32, wherein: The first reaction zone is provided with one or more than one reactor, and the reactor is one or several of a fixed bed hydrogenation reactor, a fluidized bed hydrogenation reactor and a slurry bed hydrogenation reactor.

36. The production system of claim 32, wherein: The first reaction zone is provided with two reactors, and the two reactors are connected in parallel and are switched to be used, that is, when the light lubricating oil and the first stream stop entering one of the reactors in the first reaction zone, the light lubricating oil enters the other reactor in the first reaction zone. The reactor is one or several of a fixed bed hydrogenation reactor, a fluidized bed hydrogenation reactor and a slurry bed hydrogenation reactor.

37. The production system of claim 32, wherein: The second reaction zone is provided with one or more than one reactor, and the reactor is one or several of a fixed bed hydrogenation reactor, a fluidized bed hydrogenation reactor and a slurry bed hydrogenation reactor.

38. The production system of claim 32, wherein: The second reaction zone is provided with two reactors, and the two reactors are connected in parallel and are switched to be used, that is, when the heavy lubricating oil and the second stream stop entering one of the reactors in the second reaction zone, the heavy lubricating oil enters the other reactor in the second reaction zone; and the reactor is one or several of a fixed bed hydrogenation reactor, a fluidized bed hydrogenation reactor and a slurry bed hydrogenation reactor.

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