A method and system for producing a lubricating oil base stock from a fischer-tropsch wax

Abstract

The application discloses a method and system for producing lubricating oil base oil from Fischer-Tropsch synthesis wax, wherein the Fischer-Tropsch synthesis wax is mixed with hydrogen and enters a hydrogen isomerization and condensation reaction zone to react, and the isomerization and condensation oil obtained after separation of the reaction product enters an adsorption-isomerization reaction zone to be treated by contacting with a catalyst to obtain oil phase materials; the oil phase materials are further subjected to a hydrogen refining reaction and separated to obtain light lubricating oil base oil, medium lubricating oil base oil and heavy lubricating oil base oil materials; when the refractive index of the oil phase materials is 0.1-3% higher than that of the isomerization and condensation oil, the isomerization and condensation oil stops entering the adsorption-isomerization reaction zone, and hydrogen is introduced into the adsorption-isomerization reaction zone, and the isomerization and condensation reaction occurs under the action of the catalyst and the hydrogen; the isomerization and condensation reaction product enters a hydrogen refining reaction zone to be subjected to a hydrogen refining reaction, and the reaction product is separated to obtain light lubricating oil base oil, medium lubricating oil base oil and heavy lubricating oil base oil materials.

Description

TECHNICAL FIELD

[0001] The present application belongs to the field of petrochemical industry, and relates to a production method and a production system of lubricating oil base oil, in particular to a method and a system for producing lubricating oil base oil from Fischer-Tropsch synthesis wax. BACKGROUND

[0002] At present, the overall crude oil in the world is developing in the direction of inferiority, which makes the amount of crude oil suitable for producing lubricating oil gradually decrease. Fischer-Tropsch synthesis is a process for synthesizing liquid fuels and chemicals mainly composed of long-chain alkanes from synthesis gas (CO and H2) as raw materials under the catalysis of catalysts (such as iron-based and cobalt-based) and appropriate reaction conditions. In the low-temperature Fischer-Tropsch synthesis product, the wax-containing components, including soft wax (C 20 -C 30 ) and hard wax (>C 30 ), account for more than 40%, and the main component is linear alkanes, which almost contains no sulfur, nitrogen and aromatic hydrocarbons, and is a high-quality lubricating oil base oil raw material.

[0003] The traditional production of lubricating oil base oil adopts solvent refining process, and the main steps are to remove non-ideal components such as aromatic hydrocarbons by solvent refining and to ensure the low-temperature flow performance of base oil by solvent dewaxing. In addition, clay or hydrogenation supplementary refining is generally required. However, the traditional process is restricted in development and application due to high energy consumption, heavy pollution and other factors. In recent years, the technology for producing lubricating oil by hydrogenation method has developed very rapidly. The hydrogenation process refers to the production of lubricating oil base oil by hydrogenation cracking process or hydrogenation treatment-isomerization dewaxing-hydrogenation refining combined process, which has the advantages of great flexibility of raw materials, high yield of base oil, and high economic value of by-products.

[0004] In the existing production method of high-viscosity-index lubricating oil base oil product, some methods cut the raw material into narrow fractions, and then take the narrow fractions as the feedstock of 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 the method of step-by-step isomerization dewaxing-product separation.

[0005] CN101230290A discloses a process for producing solvent oil, lubricating oil base stock and heavy wax from Fischer-Tropsch synthesis wax, comprising: a) contacting Fischer-Tropsch synthesis wax with a hydrofinishing catalyst in a hydrofinishing reaction zone I, separating the product in a distillation zone I to obtain two fractions having a final boiling point of less than 380°C to 550°C and an initial boiling point of greater than 380°C to 550°C; b) contacting the fraction having a final boiling point of less than 380°C to 550°C with a hydroisomerization catalyst in a wax hydroconversion reaction zone to produce a wax conversion oil having a reduced pour point; c) contacting the wax conversion oil with a hydrofinishing catalyst in a hydrofinishing reaction zone II and separating the product in a distillation zone II to obtain at least one solvent oil and at least one lubricating oil base stock; and d) contacting the fraction having an initial boiling point of greater than 380°C to 550°C with a hydrofinishing catalyst in a hydrofinishing reaction zone III to produce a hydrodecolorized wax. SUMMARY

[0006] In view of the problems and deficiencies in the prior art, the main object of the present application is to provide a process and system for producing lubricating oil base stock from Fischer-Tropsch synthesis wax, which first performs isomerization and pour point depression reaction on the Fischer-Tropsch synthesis wax feedstock, then selectively adsorbs the unconverted long-chain normal paraffins or long-chain isomeric paraffins with a shallow isomerization degree in the isomerization and pour point depression oil, which affect the pour point and cloud point of the product, and performs isomerization and pour point depression reaction again, and performs hydrofinishing reaction on the separated isomerization and pour point depression oil and the secondary isomerization and pour point depression product to complete hydrogenation saturation, and finally produces low-cloud-point high-viscosity-index lubricating oil base stock product.

[0007] To achieve the above object, the present application provides a process for producing lubricating oil base stock from Fischer-Tropsch synthesis wax, comprising the following steps:

[0008] (1) Fischer-Tropsch synthesis wax is mixed with hydrogen and enters a hydroisomerization and pour point depression reaction zone, and is reacted with a hydroisomerization and pour point depression catalyst, and the gaseous stream and isomerization and pour point depression oil obtained after separation of the reaction product;

[0009] (2) The isomerization and pour point depression oil obtained in step (1) enters an adsorption-isomerization reaction zone, and is treated with a catalyst to obtain an oil phase material;

[0010] (3) The oil phase material obtained after adsorption treatment in step (2) enters a hydrofinishing reaction zone with hydrogen, and is reacted with a hydrofinishing catalyst, and the reaction product is separated to obtain light lubricating oil base stock, medium lubricating oil base stock and heavy lubricating oil base stock;

[0011] (4) when the refractive index (20℃) of the oil phase material obtained in step (2) is higher than the refractive index (20℃) of the isomerized pour point depressing oil material by 0.1-3%, the isomerized pour point depressing oil material is stopped from entering the adsorption-isomerization reaction zone, and hydrogen is introduced into the adsorption-isomerization reaction zone, and the isomerized pour point depressing reaction occurs under the action of the catalyst and hydrogen, and the isomerized pour point depressing reaction product enters the hydrofining reaction zone to perform hydrofining reaction, and the reaction product, after separation, obtains light lubricating base oil, medium lubricating base oil and heavy lubricating base oil material.

[0012] Further, in the above method for producing lubricating base oil from Fischer-Tropsch synthesis wax, the Fischer-Tropsch synthesis wax is a long-chain aliphatic hydrocarbon with less side chains obtained from CO and H2 through F-T synthesis process, which is hard in texture, has a melting point usually above 100℃, low in sulfur and nitrogen content, and good in gloss.

[0013] Further, in the above method for producing lubricating base oil from Fischer-Tropsch synthesis wax, the operating conditions (isomerized pour point depressing reaction) of the hydrogen isomerized pour point depressing reaction zone in step (1) are as follows: the reaction temperature is 200-420℃, preferably 270-380℃, the reaction pressure is 1.0-20.0 MPa, preferably 3.0-15.0 MPa, the volume space velocity is 0.1-10.0 h -1 , preferably 0.5-3.0 h -1 , and the hydrogen / oil volume ratio is 100:1-1500:1, preferably 100:1-400:1.

[0014] Further, in the above method for producing lubricating base oil from Fischer-Tropsch synthesis wax, the hydrogen isomerized pour point depressing catalyst used in the hydrogen isomerized pour point depressing reaction zone in step (1) can be a commercially available product or prepared according to the existing published methods in the art. For example, the FIW-12 isomerized pour point depressing catalyst developed by Dalian Petrochemical Research Institute of PetroChina.

[0015] Further, in the above method for producing lubricating base oil from Fischer-Tropsch synthesis wax, the separation in step (1) is gas-liquid separation, and the isomerized pour point depressing reaction product is subjected to gas-liquid separation to obtain a gas phase stream and isomerized pour point depressing oil material, and the gas phase stream can be used as recycled hydrogen after purification treatment.

[0016] Further, in the above method for producing lubricating base oil from Fischer-Tropsch synthesis wax, the adsorption-isomerization reaction zone in step (2) is provided with at least one reactor, preferably 2 reactors, and further preferably 2 reactors connected in parallel and switched for use, i.e. when one reactor is switched from adsorption reaction to isomerized pour point depressing reaction, the isomerized pour point depressing oil material is switched to feed into the other reactor to ensure continuous operation of the whole device. The reactor can be one or several of the existing fixed bed hydrogenation reactor, fluidized bed hydrogenation reactor and slurry bed hydrogenation reactor, and preferably a fixed bed hydrogenation reactor.

[0017] Further, in the above-mentioned method for producing a lubricating base oil from a Fischer-Tropsch synthesis wax, the operating conditions for the adsorption reaction in the adsorption-isomerization reaction zone in step (2) are as follows: the reaction temperature is 40°C to 250°C, preferably 60°C to 200°C, the reaction pressure is 0.01 MPa to 0.5 MPa, preferably 0.08 to 0.1 MPa, and the volume space velocity is 0.05 h -1 ~ 5.0 h -1 , preferably 0.1 h -1 ~ 2.0 h -1 .

[0018] Further, in the above-mentioned method for producing a lubricating base oil from a Fischer-Tropsch synthesis wax, the catalyst comprises an intergrowth 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.

[0019] 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.

[0020] 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.

[0021] 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.

[0022] According to one embodiment of the present application, the content of the TON structure molecular sieve is 10 wt% to 80 wt%, preferably 20 wt% to 60 wt%, and the content of the 5A type molecular sieve is 1 wt% to 50 wt%, preferably 2 wt% to 20 wt%, relative to the total weight of the catalyst being 100 wt%.

[0023] According to one embodiment of the present application, the content of the mosaic molecular sieve is 10wt%-90wt%, preferably 20wt%-70wt%, based on the total weight of the catalyst being 100wt%, and the content of the active metal component is 0.05wt%-5.0wt%, preferably 0.1wt%-1.0wt%, based on the metal element.

[0024] 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.

[0025] 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.

[0026] 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.

[0027] According to one embodiment of the present application, the 5A type molecular sieve is selected from 5A molecular sieve.

[0028] 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.

[0029] 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 at least one of the sesbania powder and the starch, and the binder is an aqueous solution of inorganic acid, which can be nitric acid, etc.

[0030] 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, avoiding the occurrence of excessive isomerization phenomenon.

[0031] According to one embodiment of the present application, the preparation method of the mosaic molecular sieve comprises the following steps:

[0032] (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

[0033] (2) hydrothermally crystallizing the gel mixture, and then washing, drying and calcining to obtain a first mosaic molecular sieve.

[0034] According to one embodiment of the present application, the preparation method further comprises the following steps:

[0035] (3) calcium-exchanging the first mosaic molecular sieve, and then washing, drying and calcining to obtain a second mosaic molecular sieve.

[0036] According to one embodiment of the present application, in step (1), the silicon source is at least one selected from water glass, sodium silicate, methyl orthosilicate, ethyl orthosilicate, propyl orthosilicate and butyl orthosilicate.

[0037] According to one embodiment of the present application, in step (1), the alkali source is at least one selected from alkali metal hydroxides, preferably sodium hydroxide.

[0038] According to one embodiment of the present application, in step (1), the aluminum source is at least one selected from sodium metaaluminate, aluminum isopropoxide, aluminum sulfate, aluminum hydroxide, aluminum oxide and pseudo-boehmite.

[0039] According to one embodiment of the present application, in step (1), the template agent is at least one selected from polyethylene oxide triblock copolymer (P123) and dimethyloctadecyl [3- (trimethoxysilyl) propyl] ammonium chloride (TPOAC).

[0040] According to one embodiment of the present application, in step (1), the TON structure molecular sieve is one or more selected from ZSM-22, Theta-1, ISI-1, KZ-2 and NU-10, preferably ZSM-22.

[0041] According to one embodiment of the present application, in step (1), the operation conditions of the contacting include: temperature of 15-30℃ and time of 1-4h under stirring.

[0042] According to one embodiment of the present application, in step (1), the molar ratio of the alkali source (calculated as 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.

[0043] 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.

[0044] According to one embodiment of the present application, in step (2), the drying temperature is 80-200℃ and the drying time is 2-24h.

[0045] According to one embodiment of the present application, in step (2), the calcination temperature is 400-600°C, and the calcination time is 2-12 hours.

[0046] According to one embodiment of the present application, in step (3), the operation conditions for calcium exchange include: the exchange temperature is 60-100°C, the exchange time is 1-12 hours, and the calcium ion concentration in the calcium exchange solution is 0.1-2.5 mol / L.

[0047] According to one embodiment of the present application, in step (3), the drying temperature is 80-150°C, and the drying time is 2-12 hours.

[0048] According to one embodiment of the present application, in step (3), the calcination temperature is 300-500°C, and the calcination time is 2-8 hours.

[0049] Further, in the above method for producing lubricating oil base oil from Fischer-Tropsch synthesis wax, the operation conditions of the hydrofining reaction zone in step (3) are: the reaction temperature is 180-300°C, preferably 200-260°C, the hydrogen partial pressure is 2.0-18.0 MPa, preferably 10.0-15.0 MPa, the volume space velocity is 0.2-6.0 h-1, preferably 0.3-1.8 h-1, and the hydrogen / oil volume ratio is 400:1-1500:1, preferably 600:1-800:1.

[0050] Further, in the above method for producing lubricating oil base oil from Fischer-Tropsch synthesis wax, the hydrofining catalyst used in the hydrofining reaction zone in step (3) can be a commercially available product or prepared according to the existing published methods in the art. For example, the FMTA-2 hydrofining catalyst developed by Dalian Petrochemical Research Institute of PetroChina.

[0051] Further, in the above method for producing lubricating oil base oil from Fischer-Tropsch synthesis wax, in step (4), when the refractive index (20°C) of the oil phase material obtained in step (2) is 0.3-2.0% higher than that of the isomerization pour point depressing oil material, the isomerization pour point depressing oil material is stopped from entering the adsorption-isomerization reaction zone.

[0052] Further, in the above method for producing lubricating oil base oil from Fischer-Tropsch synthesis wax, in step (4), the operation conditions of the isomerization pour point depressing reaction in the adsorption-isomerization reaction zone are: the reaction temperature is 200-420°C, preferably 270-380°C, the reaction pressure is 1.0-20.0 MPa, preferably 3.0-15.0 MPa, the volume space velocity is 0.1-10.0 h -1 , preferably 0.5-3.0 h -1The hydrogen to oil volume ratio is 100:1 to 1500:1, preferably 100:1 to 400:1.

[0053] Further, in the method for producing lubricating base oil from Fischer-Tropsch synthesis wax, the separation in step (3) and step (4) comprises two processes of gas-liquid separation and fractionation, the reaction product is firstly subjected to gas-liquid separation, and after the separation, a gas phase stream and a liquid phase stream are obtained, the gas phase stream can be recycled as recycled hydrogen after being subjected to purification treatment; the liquid phase stream is further subjected to separation in a fractionation column, and after the separation, light lubricating base oil, medium lubricating base oil and heavy lubricating base oil are obtained.

[0054] Further, in the method for producing lubricating base oil from Fischer-Tropsch synthesis wax, the heavy lubricating base oil obtained by the separation in the fractionation column can be recycled in whole or in part back to the adsorption-isomerization reaction zone.

[0055] The second aspect of the present application provides a system for producing lubricating base oil from Fischer-Tropsch synthesis wax, comprising:

[0056] a hydrogen isomerization dewaxing reaction zone, which is used for receiving hydrogen and Fischer-Tropsch synthesis wax, and the Fischer-Tropsch synthesis wax and the hydrogen are reacted in contact with a hydrogen isomerization dewaxing catalyst;

[0057] a first gas-liquid separation unit, which is used for receiving and separating the reaction product from the hydrogen isomerization dewaxing reaction zone, and after the separation, a gas phase stream and an isomerization dewaxing oil are obtained;

[0058] an adsorption-isomerization reaction zone, which is used for receiving the isomerization dewaxing oil from the gas-liquid separation unit, and the isomerization dewaxing oil is treated in contact with an adsorbent, and after the treatment, an oil phase material is obtained; when the refractive index (20℃) of the oil phase material is 0.1 to 3% higher than the refractive index (20℃) of the isomerization dewaxing oil, the isomerization dewaxing oil is stopped from entering the adsorption-isomerization reaction zone, and at the same time, hydrogen is introduced into the adsorption-isomerization reaction zone, and under the action of the adsorbent and the hydrogen, an isomerization dewaxing reaction product is obtained;

[0059] a hydrogen refining reaction zone, which is used for receiving the oil phase material and the isomerization dewaxing reaction product from the adsorption-isomerization reaction zone, and the oil phase material and the isomerization dewaxing reaction product are reacted in contact with a hydrogen refining catalyst, and a hydrogen refining reaction product is obtained;

[0060] a second gas-liquid separation unit, which is used for receiving the hydrogen refining reaction product from the hydrogen refining reaction zone, and after the separation, a gas phase stream and a liquid phase stream are obtained;

[0061] a fractionation column, which is used for receiving the liquid phase stream from the second gas-liquid separation unit, and after the fractionation, light lubricating base oil, medium lubricating base oil and heavy lubricating base oil are obtained.

[0062] Further, in the system for producing lubricating base oil from Fischer-Tropsch synthesis wax, the adsorption-isomerization reaction zone is provided with at least one reactor, preferably two reactors, and further preferably two reactors are connected in parallel and switched for use, i.e. when one reactor is switched from adsorption reaction to isomerization and condensation reaction, the isomerization and condensation oil is switched to feed into the other reactor, ensuring continuous operation of the entire device. The reactor can use one or more of the existing fixed bed hydrogenation reactor, fluidized bed hydrogenation reactor, slurry bed hydrogenation reactor, preferably a fixed bed hydrogenation reactor.

[0063] Further, in the system for producing lubricating base oil from Fischer-Tropsch synthesis wax, the first gas-liquid separation unit can use any device in the art that can achieve gas-liquid two-phase separation function, such as a gas-liquid separator, a flash tower, etc.

[0064] Further, in the system for producing lubricating base oil from Fischer-Tropsch synthesis wax, the second gas-liquid separation unit can use any device in the art that can achieve gas-liquid two-phase separation function, such as a gas-liquid separator, a flash tower, etc.

[0065] Further, in the system for producing lubricating base oil from Fischer-Tropsch synthesis wax, the gas phase stream separated by the first gas-liquid separation unit and the second gas-liquid separation unit is purified and then used as circulating hydrogen through pipelines to the adsorption-isomerization reaction zone, the hydrofining reaction zone, and the hydrogenation isomerization and condensation reaction zone.

[0066] Further, in the system for producing lubricating base oil from Fischer-Tropsch synthesis wax, the heavy lubricating base oil separated by the fractionating column is recycled to the adsorption-isomerization reaction zone through pipelines.

[0067] Compared with the prior art, the method and system for producing lubricating base oil from Fischer-Tropsch synthesis wax provided by the present application have the following advantages:

[0068] 1. The method for producing lubricating oil base oil from Fischer-Tropsch synthesis wax provided by the present application, by performing secondary adsorption treatment on the Fischer-Tropsch synthesis wax after hydroisomerization dewaxing, separating the highly isomerized long-chain isomeric alkanes, and only performing isomerization dewaxing reaction on the components affecting the turbidity of the oil product, such as the unconverted long-chain normal alkanes or the long-chain isomeric alkanes with a shallow isomerization degree, to further produce low-turbidity lubricating oil base oil products, thereby reducing the isomerization dewaxing processing load, reducing the device investment, reducing the hydrogen consumption, and improving the economic efficiency of the device. Moreover, the applicant found that, in the currently used hydroisomerization dewaxing catalyst, the addition of 5A molecular sieve has a selective adsorption effect on the Fischer-Tropsch synthesis wax in the absence of hydrogen, which can effectively separate the long-chain normal alkanes or the long-chain isomeric alkanes with a shallow isomerization degree from the highly isomerized long-chain isomeric alkanes, thereby reducing the high-turbidity group content of the lubricating oil base oil products from the raw material aspect and reducing the turbidity of the lubricating oil base oil products.

[0069] 2. The molecular sieve composition provided by the present application is combined by 5A molecular sieve and TON structure molecular sieve through the interpenetration of each other, wherein the 5A molecular sieve has good adsorption function and can enrich alkanes, the TON structure molecular sieve has specific pore structure and suitable acidity, which is beneficial to the selective isomerization of alkanes, and the molecular sieve composition provided by the present application has the above specific functions, and still maintains good adsorption performance after loading active metals. After the catalyst prepared by using the molecular sieve composition provided by the present application as a component is subjected to isomerization reaction and regeneration, the molecular sieve still maintains good stability.

[0070] 3. The method for producing lubricating oil base oil from Fischer-Tropsch synthesis wax provided by the present application, by using the catalyst which has the selective adsorption ability to long-chain isomeric alkanes, long-chain monocyclic naphthenes and long-chain monocyclic aromatics and the ability to selectively isomerize alkanes in the presence of hydrogen and under suitable reaction conditions, the production process of the lubricating oil base oil is simplified, the device investment is reduced, and the hydrogen consumption is reduced. BRIEF DESCRIPTION OF DRAWINGS

[0071] Figure 1 The flowchart of the method for producing lubricating oil base oil from Fischer-Tropsch synthesis wax provided by the present application is shown. DETAILED DESCRIPTION

[0072] The present application will be further described in combination with the drawings and specific examples. The following examples will further illustrate the method provided by the present application, but do not limit the scope of the present application.

[0073] Unless specifically stated otherwise, the term "comprising" encompasses the presence of stated elements or components but not the exclusion of others. The term "consisting essentially of" when used in a claim, should not be construed as providing a strict

[0074] In this document, relational terms such as "first," "second," and the like can be used solely to distinguish one entity or action from another entity or action, without necessarily implying any actual such relationship or order. In this document, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but can include other elements not expressly listed or inherent to such process, method, article, or apparatus. An element proceeded by "comprises a" does not, without more constraints, exclude the presence of additional elements of the same type in the composition. In this document, the terms "first," "second," and the like can be used to describe various elements, but do not necessarily have to be used in all cases in this description.

[0075] In this document, the terms "first," "second," and the like can be used solely to distinguish one entity or action from another entity or action, without necessarily implying any actual such relationship or order. In this document, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but can include other elements not expressly listed or inherent to such process, method, article, or apparatus. An element proceeded by "comprises a" does not, without more constraints, exclude the presence of additional elements of the same type in the composition. In this document, the terms "first," "second," and the like can be used to describe various elements, but do not necessarily have to be used in all cases in this description.

[0076] In this document, all numerical values of parameters (e.g., of quantities or conditions) are to be understood as modified in all instances by the term "about" unless otherwise indicated. In this document, the use of "or" means "and / or" unless stated otherwise. Furthermore, in the description of the application, the use of "a" or "an" means "one or more" unless otherwise indicated.

[0077] In the context of the present specification, unless explicitly stated otherwise, both the silicon-aluminum material and the catalyst are subjected to a calcination treatment before measurement, sometimes referred to as "calcined form". Here, the conditions of the calcination treatment include a calcination temperature of 600°C and a calcination time of 3 hours or more in an air atmosphere.

[0078] In the context of the present specification, long-side-chain hydrocarbons refer specifically to one or more of long-side-chain isomeric alkanes, long-side-chain monocyclic naphthenes, and long-side-chain monocyclic aromatics, excluding other hydrocarbons with long-side-chains. In addition, according to the present application, by long-side-chain is meant a C8-22 (preferably C10-18) straight-chain alkyl group as the side chain.

[0079] In the context of the present specification, a mechanical mixture refers to a mixture of two or more materials obtained by mechanical mixing. Here, the mechanical mixing includes simple mixing, grinding, pulping, and the like.

[0080] In the context of the present specification, the mosaic molecular sieve refers to one or more kinds of molecular sieve crystals in which the surface or interior is inlaid with another one or more kinds of molecular sieve, and is a composite crystal having two or more kinds of molecular sieve structural characteristics. Compared with a mechanical mixture, the combination of different molecular sieves in the mosaic structure is more compact, and a truly integrated composite structure at the molecular level is formed.

[0081] In the context of the present specification, the refractive index is represented by a Mettler refractometer R5, the long-chain hydrocarbon content is represented by an Agilent gas chromatograph 7890, the XRD pattern of the sample is represented by a D / max-2500 full-automatic rotating target X-ray diffractometer, the specific surface area, pore volume and average pore diameter of the mosaic molecular sieve and the specific surface area, pore volume and average pore diameter of the catalyst are tested and represented by an ASAP 2405 physical adsorption instrument through a N2 adsorption-desorption method, and the calcium content of the calcium-type molecular sieve is represented by X-ray fluorescence diffraction.

[0082] In the context of the present specification, the TON structure molecular sieve content in the mosaic molecular sieve is quantitatively analyzed by XRD determination.

[0083] Unless specifically indicated otherwise, all percentages, parts, ratios, etc. mentioned in the present specification are based on weight, the pressure is gauge pressure, and the weight or content is on a dry basis.

[0084] For example, the catalysts of the present application can be used in the preparation of a compound of formula (I) by reacting a compound of formula (II) with a compound of formula (III) in the presence of a catalyst of the present application. Figure 1As shown, the method for producing lubricating oil base oil from Fischer-Tropsch synthesis wax provided by the present application specifically includes the following steps: Fischer-Tropsch synthesis wax 1 and hydrogen 20 are mixed and introduced into a hydroisomerization dewaxing reaction zone 2, and react with a hydroisomerization dewaxing catalyst; the reaction product 3 is introduced into a first gas-liquid separation unit 4 for separation, and a first gas phase stream 5 and an isomerization dewaxing oil 6 are obtained after separation; the isomerization dewaxing oil 6 is introduced into an adsorption-isomerization reaction zone, which is provided with two reactors, namely a first reactor 7 and a second reactor 8, and the first reactor 7 and the second reactor 8 are connected in parallel and switched for use, and switching is realized by a control valve (not shown in the figure); the isomerization dewaxing oil 6 is first introduced into the first reactor 7, and reacts with a catalyst to be treated; the oil phase material 9 obtained after adsorption treatment is introduced into a hydrofining reaction zone 11 together with hydrogen 20, and reacts with a hydrofining catalyst; the hydrofining reaction product 12 is introduced into a second gas-liquid separation unit 13 for separation, and a second gas phase stream 14 and a liquid phase stream 15 are obtained after separation; the liquid phase stream 15 is introduced into a fractionating column 16, and light lubricating oil base oil 17, medium lubricating oil base oil 18 and heavy lubricating oil base oil 19 are obtained after separation. When the refractive index (20℃) of the oil phase material 9 is 0.1-3% higher than the refractive index (20℃) of the isomerization dewaxing oil 6, the isomerization dewaxing oil 6 is stopped from being introduced into the first reactor 7, and is switched to be introduced into the second reactor 8, and hydrogen 20 is introduced into the first reactor 7 at the same time, and the isomerization dewaxing reaction occurs under the action of the catalyst, and the isomerization dewaxing reaction product 10 is introduced into the hydrofining reaction zone 11 for hydrofining reaction, and the reaction product is separated to obtain light lubricating oil base oil 17, medium lubricating oil base oil 18 and heavy lubricating oil base oil 19.

[0085] The properties of the raw oil Fischer-Tropsch synthesis wax used in the method embodiments and the comparative example of the present application are shown in Table 1. The isomerization dewaxing catalyst and the hydrofining catalyst involved in Examples 1-2 and the comparative example can be selected from commercial catalysts according to properties, or can be prepared according to the knowledge in the art. In the method of the present application, the specific physical and chemical properties of the isomerization dewaxing catalyst and the hydrofining catalyst are shown in Table 2.

[0086] Table 1 Properties of raw oil

[0087]

[0088] Table 2 Physical and chemical properties of catalysts

[0089]

[0090] In the present application, the catalyst used is prepared by the following method, and the properties of the obtained adsorbent are shown in Table 3.

[0091] Example 1

[0092] Preparation of catalyst CAT-1:

[0093] A mixture of 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 was uniformly mixed and loaded into a crystallization kettle, 300 g of ZSM-22 molecular sieve was added and stirred, then the reaction kettle was sealed, heated to 110°C and hydrothermally crystallized for 6 h. After crystallization was completed, the product obtained by crystallization was washed, then dried at 110°C for 6 h, and then calcined at 500°C for 5 h, thereby obtaining a first mosaic molecular sieve Z2. Then the molecular sieve Z2 was ion exchanged in a 1.8 mol / L CaCl2 solution at 90°C for 4 h, suction filtered and washed, then dried at 100°C for 4 h, and then calcined at 400°C for 3 h, thereby obtaining a second mosaic molecular sieve GZ-1, which has a specific surface area of 452 m2 / g, a pore volume of 0.25 mL / g, and a TON structure molecular sieve mass fraction of 85%. 2

[0094] A mixture of 210 g of the eutectic molecular sieve GZ-1 prepared above, 90 g of pseudoboehmite (dry basis) and 20 g of sesbania powder was uniformly mixed, 9 ml of concentrated nitric acid (65% by mass) and an appropriate amount of water were added, and the mixture was thoroughly kneaded and then extruded into strips. The formed carrier was dried at 100°C for 4 h and calcined at 550°C for 4 h to obtain a carrier ES-1. Then, a noble metal Pt was impregnated by a saturation impregnation method, the Pt loading amount was 0.50% by mass of the carrier, and the catalyst of the application was obtained after drying at 100°C for 6 h and calcining at 500°C for 3 h, and the number was CAT-1.

[0095] Example 2

[0096] Preparation of catalyst CAT-2

[0097] A mixture of 64 g of sodium hydroxide, 208 g of tetraethyl orthosilicate, 98.4 g of sodium metaaluminate, 24.8 g of dimethyloctadecyl[3-(trimethoxysilyl)propyl]ammonium chloride (TPOAC) and 2700 g of water was uniformly mixed and loaded into a crystallization kettle, 240 g of ZSM-22 molecular sieve was added and stirred, then the reaction kettle was sealed, heated to 100°C and hydrothermally crystallized for 7 h. After crystallization was completed, the product obtained by crystallization was washed, then dried at 100°C for 6 h, and then calcined at 450°C for 8 h, thereby obtaining a first mosaic molecular sieve Z6. Then the molecular sieve Z6 was ion exchanged in a 1.5 mol / L CaCl2 solution at 80°C for 4 h, suction filtered and washed, then dried at 100°C for 5 h, and then calcined at 350°C for 6 h, thereby obtaining a second mosaic molecular sieve GZ-2, which has a specific surface area of 498 m2 / g, a pore volume of 0.23 mL / g, and a TON structure molecular sieve mass fraction of 82%. ​

[0098] The preparation process of the catalyst CAT-2 of the present invention is the same as that in Example 1, except that the embedded molecular sieve used is GZ-2 and the Pt loading is 0.48 wt% of the support, thus preparing the catalyst CAT-2 of the present invention.

[0099] Example 3

[0100] Preparation of catalyst CAT-3

[0101] 80g sodium hydroxide, 184g sodium silicate, 65.6g sodium aluminate, 4.96g dimethyloctadecyl[3-(trimethoxysilyl)propyl]ammonium chloride (TPOAC), and 540g water were mixed evenly and placed into a crystallization vessel. Then, 42g of ZSM-22 molecular sieve was added and stirred. The vessel was sealed, and the temperature was raised to 120℃ for hydrothermal crystallization for 5 hours. After crystallization, the product was washed, dried at 120℃ for 5 hours, and then calcined at 500℃ for 4 hours to obtain the first embedded molecular sieve Z3. Then, molecular sieve Z3 was subjected to ion exchange in a 1.2 mol / L CaCl2 solution at 70℃ for 6 h, filtered and washed, dried at 100℃ for 4 h, and then calcined at 450℃ for 3 h to obtain the second embedded molecular sieve GZ-3, which has a specific surface area of ​​573 m2 / g, a pore volume of 0.19 mL / g, and a TON structure molecular sieve mass fraction of 47%.

[0102] The preparation process of catalyst 3 of the present invention is the same as that in Example 1, except that the embedded molecular sieve used is GZ-3, the Pt loading is 0.31 wt% of the support, and the catalyst CAT-3 of the present invention is prepared.

[0103] Table 2 Physicochemical properties of catalysts

[0104]

[0105] Example 4

[0106] Using the feedstock oils listed in Table 1, Figure 1 The process flow described above uses catalyst CAT-1 in the adsorption-isomerization reaction zone. The process conditions are shown in Table 3.

[0107] Example 5 - Implementation 6

[0108] Using the raw materials listed in Table 1, Figure 1 The process flow described above uses catalysts CAT-2 and CAT-3 in the adsorption-isomerization reaction zone, respectively. The process conditions are shown in Table 3.

[0109] Comparative Example 1

[0110] ZSM-22 molecular sieve (Si / Al ratio 90) 134 g, 5A molecular sieve 200 g and 150 g (as Al2O3) 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, 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 h, and then calcined at 550 ℃ for 4 h in an air atmosphere to obtain the catalyst carrier of the application.

[0111] 300 g of the carrier was loaded with noble metal Pt by saturated impregnation, then dried at 110 ℃ for 7 h, and calcined at 500 ℃ for 3 h in an air atmosphere to obtain the catalyst of the 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 polyoxyethylene tri-block 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 crystallization, 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 the first inlaid 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 the second inlaid molecular sieve D.

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

[0115] Comparative Example 3 and Comparative Example 4

[0116] The raw materials listed in Table 1 were used, and the process flow shown in Table 1 was used, and the catalysts C-D1 and C-D2 were used in the adsorption-isomerization reaction zone, and the process conditions are shown in Table 3. Figure 1 The results are shown in Table 3.

[0117] Table 3 Process conditions and results of examples and comparative examples

[0118] Example number Example 4 Example 5 Example 6 Comparative Example 3 Comparative Example 4 Isodewaxing process conditions Reaction temperature / °C 350 410 265 350 350 Reaction pressure / MPa 12.0 2.5 17.5 12.0 12.0 Hydrogen to oil volume ratio 400 1200 800 400 400 Volume space velocity / h -1 ]] 1.0 0.20 4.20 1.0 1.0 Isodewaxing stream refractive index (20 °C) 1.4102 1.4088 1.4065 1.4102 1.4102 Adsorption reaction process conditions in the adsorption-isomerization reaction zone Adsorption temperature / °C 130 55 230 130 130 Adsorption pressure / MPa 0.09 0.40 0.05 0.09 0.09 Volume space velocity / h -1 ]] 1.1 0.08 4.50 1.1 1.1 Refractive index of oil phase material (20 °C) 1.4271 1.4116 1.4416 1.4271 1.4271 Isodewaxing process conditions in the adsorption-isomerization reaction zone Reaction temperature / °C 340 400 255 345 345 Reaction pressure / MPa 12.0 2.5 17.5 12.0 12.0 Hydrogen to oil volume ratio 400 1000 600 400 400 Volume space velocity / h -1 ]] 1.2 0.30 4.50 1.2 1.2 Hydrofinishing process conditions Reaction temperature / °C 240 180 270 240 240 Reaction pressure / MPa 12.0 2.5 17.5 12.0 12.0 Hydrogen to oil volume ratio 800 500 1200 800 800 Volume space velocity / h -1 ]] 1.20 0.25 5.50 1.20 1.20 Base oil properties Light lubricating oil base oil Pour point / °C -32 -30 -24 -20 -15 Cloud point / °C -5 -2 1 3 7 Viscosity (100°C), mm / s 2 ]] 3.96 4.01 3.95 4.08 4.10 Viscosity index 149 147 145 143 138 Medium lubricating oil base oil Pour point / °C -27 -25 -21 -16 -12 Cloud point / °C -2 0 5 6 10 Viscosity (100°C), mm / s 2 ]] 5.89 5.92 6.00 6.02 5.96 Viscosity index 153 150 148 146 140 Heavy lubricating oil base oil Pour point / °C -24 -25 -18 -12 -8 Cloud point / °C 1 3 8 10 15 Viscosity (100°C), mm / s 2 ]] 9.53 9.56 9.63 9.59 9.70 Viscosity index 157 155 154 151 147

Claims

1. A method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax, comprising the following steps: (1) Fischer-Tropsch synthesis wax is mixed with hydrogen and enters the hydroisomerization dewaxing reaction zone, where it reacts with the hydroisomerization dewaxing catalyst. The reaction products are separated to obtain gaseous stream and isomerized dewaxing oil. (2) The isomerized pour point depressed oil obtained in step (1) enters the adsorption-isomerization reaction zone and is treated by contacting the catalyst to obtain the oil phase material; the operating conditions of the adsorption reaction in the adsorption-isomerization reaction zone are: reaction temperature of 40℃~250℃, reaction pressure of 0.01MPa~0.5MPa, and volume hourly space velocity of 0.05h. -1 ~5.0h -1 ; (3) The oil phase material obtained after the adsorption treatment in step (2) enters the hydrorefining reaction zone with hydrogen and reacts with the hydrorefining catalyst. The reaction products are separated to obtain light lubricating oil base oil, medium lubricating oil base oil and heavy lubricating oil base oil. (4) When the refractive index of the oil phase material obtained in step (2) at 20°C is 0.1-3% higher than that of the isomerized pour point depressed oil at 20°C, stop the isomerized pour point depressed oil from entering the adsorption-isomerization reaction zone. At the same time, hydrogen is introduced into the adsorption-isomerization reaction zone. Under the action of the catalyst and hydrogen, the isomerization pour point depressed reaction occurs. The isomerization pour point depressed reaction product enters the hydrorefining reaction zone for hydrorefining reaction. After separation, the reaction product is used to obtain light lubricating oil base oil, medium lubricating oil base oil and heavy lubricating oil base oil. The catalyst described in steps (2) and (4) comprises an embedded molecular sieve of TON structure molecular sieve and 5A type molecular sieve, an active metal component, and an inorganic refractory oxide; the active metal component is selected from at least one of the noble metals in Group VIII of the periodic table.

2. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The operating conditions of the hydroisomerization dewaxing reaction zone in step (1) are as follows: reaction temperature 200–420℃, reaction pressure 1.0–20.0 MPa, and volume hourly space velocity 0.1–10.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is 100:1 to 1500:

1.

3. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The operating conditions of the hydroisomerization dewaxing reaction zone in step (1) are as follows: reaction temperature 270–380℃, reaction pressure 3.0–15.0 MPa, and volume hourly space velocity 0.5–3.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is 100:1 to 400:

1.

4. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, In step (2), at least one reactor is set up in the adsorption-isomerization reaction zone.

5. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, In step (2), two reactors are set up in the adsorption-isolation reaction zone. The two reactors are connected in parallel and can be switched for use. That is, when one reactor switches from the adsorption reaction to the isomerization dewaxing reaction process, the isomerization dewaxing oil is switched to the other reactor to ensure the continuous operation of the entire device.

6. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The operating conditions for the adsorption reaction in the adsorption-isomerization reaction zone in step (2) are: reaction temperature of 60℃~200℃, reaction pressure of 0.08~0.1MPa, and volume hourly space velocity of 0.1h. -1 ~2.0h -1 .

7. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, TON structured molecular sieves are embedded on at least a portion of the surface of the 5A type molecular sieve with a predetermined surface coverage, wherein a suitable surface coverage is greater than 0.5% and less than 50%.

8. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, TON structured molecular sieves are embedded on at least a portion of the surface of the 5A type molecular sieve with a predetermined surface coverage, wherein a suitable surface coverage is greater than 0.5% and less than 20%.

9. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, TON structured molecular sieves are embedded on at least a portion of the surface of the 5A type molecular sieve with a predetermined surface coverage, wherein a suitable surface coverage is more than 1% and less than 50%.

10. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, TON structured molecular sieves are embedded on at least a portion of the surface of the 5A type molecular sieve with a predetermined surface coverage, wherein a suitable surface coverage is more than 1% and less than 20%.

11. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The specific surface area of ​​the embedded molecular sieve is 300 m². 2 / g~600m 2 / g, pore volume 0.15cm 3 / g~0.40cm 3 / g.

12. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The catalyst has a specific surface area of ​​200 m². 2 / g~550m 2 / g, pore volume 0.25 cm³ 3 / g~0.60 cm 3 / g.

13. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The weight ratio of 5A molecular sieve to TON structured molecular sieve is 1:80-3:

1.

14. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The weight ratio of 5A molecular sieve to TON structured molecular sieve is 1:30-1:

1.

15. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, Based on a total catalyst weight of 100wt%, the content of the embedded molecular sieve is 10wt%-90wt%, and the content of the active metal component, calculated as metal element, is 0.05wt%-5.0wt%.

16. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, Based on a total catalyst weight of 100wt%, the content of the embedded molecular sieve is 20wt%-70wt%, and the content of the active metal component, calculated as metal element, is 0.1wt%-1.0wt%.

17. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The inorganic refractory oxide is selected from one or more of aluminum oxide, titanium oxide, boron oxide, silicon oxide, zirconium oxide, and magnesium oxide.

18. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The inorganic refractory oxide is aluminum oxide.

19. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The active metal component is selected from at least one of Pt and Pd.

20. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The active metal component is Pt.

21. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, TON structure molecules were screened from one or more of ZSM-22, Theta-1, ISI-1, KZ-2, and NU-10; 5A type molecules were screened from 5A molecular sieves.

22. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The TON structure molecular sieve is ZSM-22; the 5A type molecular sieve is derived from the 5A molecular sieve.

23. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The operating conditions of the hydrogenation refining reaction zone in step (3) are as follows: reaction temperature 180℃~300℃, hydrogen partial pressure 2.0MPa~18.0MPa, and volume hourly space velocity 0.2h. -1 ~6.0h -1 The hydrogen-to-oil volume ratio is 400:1 to 1500:

1.

24. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The operating conditions of the hydrorefining reaction zone in step (3) are as follows: reaction temperature 200℃~260℃, hydrogen partial pressure 10.0~15.0MPa, and volume hourly space velocity 0.3 h⁻¹. -1 ~1.8h -1 The hydrogen-to-oil volume ratio is 600:1 to 800:

1.

25. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, In step (4), when the refractive index of the oil phase material obtained in step (2) at 20°C is 0.3 to 2.0% higher than that of the isomerized pour point depressed oil at 20°C, the isomerized pour point depressed oil is stopped from entering the adsorption-isomerization reaction zone.

26. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The operating conditions for the isomerization-decondensation reaction in the adsorption-isomerization reaction zone in step (4) are: reaction temperature of 200–420℃, reaction pressure of 1.0–20.0 MPa, and volume hourly space velocity of 0.1–10.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is 100:1 to 1500:

1.

27. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, The operating conditions for the isomerization-decondensation reaction in the adsorption-isomerization reaction zone in step (4) are: reaction temperature of 270–380℃, reaction pressure of 3.0–15.0 MPa, and volume hourly space velocity of 0.5–3.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is 100:1 to 400:

1.

28. The method for producing lubricating oil base oil from Fischer-Tropsch synthetic wax according to claim 1, wherein, Heavy lubricating oil base oils are recycled in whole or in part back to the adsorption-isomerization reaction zone for treatment.

29. A system for implementing the method of producing lubricating oil base oil from Fischer-Tropsch synthetic wax as described in any one of claims 1-28, comprising: The hydroisomerization dewaxing reaction zone is used to receive hydrogen and Fischer-Tropsch synthesis wax. The Fischer-Tropsch synthesis wax, hydrogen and hydroisomerization dewaxing catalyst are in contact to react. The first gas-liquid separation unit is used to receive and separate the reaction products from the hydroisomerization dewaxing reaction zone, and the gaseous stream and isomerized dewaxing oil obtained after separation. The adsorption-isomerization reaction zone is used to receive isomerized pour point depressed oil from the gas-liquid separation unit, which is then treated by contacting the adsorbent to obtain the oil phase material. When the refractive index of the oil phase material at 20℃ is 0.1-3% higher than that of the isomerized pour point depressed oil at 20℃, the flow of the isomerized pour point depressed oil into the adsorption-isomerization reaction zone is stopped, and hydrogen is introduced into the adsorption-isomerization reaction zone. Under the action of the adsorbent and hydrogen, an isomerization-isomerization reaction occurs to obtain the isomerization-isomerization reaction product. The hydrorefining reaction zone is used to receive oil phase materials and isomerization dewaxing reaction products from the adsorption-isomerization reaction zone, and to react them in contact with hydrogen and the hydrorefining catalyst to obtain the hydrorefining reaction products. The second gas-liquid separation unit is used to receive the hydrorefining reaction products from the hydrorefining reaction zone and separate them into gaseous and liquid streams. The fractionation tower is used to receive the liquid feed stream from the second gas-liquid separation unit and obtain light lubricating oil base oil, medium lubricating oil base oil and heavy lubricating oil base oil after fractionation.

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