Lubricating oil base oil and preparation method thereof

Abstract

The invention provides lubricant base oil and a preparation method thereof, and the preparation method comprises the following steps: carrying out a hydroisomerization reaction on Fischer-Tropsch wax with a distillation range of 400-550 DEG C under the action of a hydroisomerization catalyst, and then carrying out a hydrofining reaction and rectification under the action of a hydrofining catalyst to obtain the lubricant base oil, the preparation method of the hydroisomerization catalyst comprises the following steps: synthesizing a ZSM-48 seed crystal, preparing a ZSM-48 molecular sieve, forming a carrier, loading noble metal ions, roasting and the like. The hydroisomerization catalyst shows high isomerization selectivity for Fischer-Tropsch wax with a distillation range of 400-550 DEG C, and lubricating oil base oil with high viscosity index, low pour point and low cloud point can be prepared from the catalyst under the action of the hydroisomerization catalyst. The method for preparing the lubricant base oil not only has the advantages of high yield and simple preparation process flow, but also can produce high-quality 4cSt base oil and 6cSt base oil at the same time.

Description

Technical Field

[0001] The present invention relates to the field of coal chemical industry, and in particular to a lubricating oil base oil and a preparation method thereof. Background Art

[0002] The indirect coal liquefaction process refers to the process of generating oil products and chemicals through gasification, transformation, purification, Fischer-Tropsch synthesis reaction, etc. The intermediate products of Fischer-Tropsch synthesis are rich in olefins, and are mainly straight-chain alkanes after hydrogenation and saturation. The saturated hydrocarbon content in the hydrogenated Fischer-Tropsch wax is ≥90%, and there are basically no impurities such as aromatics, sulfur, and nitrogen, which is suitable for the production of high-quality, high-value-added lubricant base oil products.

[0003] CN111690434A discloses a method for preparing lubricating oil base oil from Fischer-Tropsch wax and lubricating oil base oil, wherein the method firstly hydrocracking the Fischer-Tropsch wax to obtain cracked base oil, then distilling the cracked base oil to obtain fraction i at 370-430°C and fraction ii greater than 430°C, then hydroisomerizing the fraction i or a mixture of fraction i and the processed fraction to obtain isomerized base oil; finally, dewaxing and refining the isomerized base oil to obtain wax conversion oil, and then distilling to obtain lubricating oil base oil. This method can produce high-viscosity base oil, but its yield for low-viscosity base oil is low. In addition, this method also has the problem of complex preparation process.

[0004] CN102533329A discloses a method for producing lubricating oil base oil from Fischer-Tropsch wax. The synthesis method comprises: a) contacting and reacting the Fischer-Tropsch wax with a hydrorefining catalyst in a hydrorefining reaction zone I to obtain a Fischer-Tropsch wax after hydrogenation olefin saturation and deoxygenation; b) contacting and reacting the Fischer-Tropsch wax obtained in step a) with a hydroisomerization catalyst in a wax hydroconversion reaction zone A to obtain a wax conversion product oil with a reduced pour point; c) contacting the wax conversion product oil obtained in step b) with a hydroisomerization catalyst in a wax hydroconversion reaction zone B to obtain a wax conversion product oil with a further reduced pour point; d) contacting the wax conversion product oil with a further reduced pour point obtained in step c) with a hydrorefining catalyst in a hydrorefining reaction zone II to obtain a wax conversion product oil after hydrorefining; and e) separating the product oil obtained in step d) in a distillation zone to obtain a lubricating oil base oil. This method can appropriately increase the base oil yield by gradually slowing down the pour point through two isomerization reaction zones. However, since the Fischer-Tropsch wax contains a large amount of normal alkanes with a high carbon number, excessive cracking reaction will still occur if it enters the isomerization reaction zone directly, resulting in a decrease in the lubricant base oil yield and a lower viscosity index.

[0005] CN1761734A discloses a method for producing base oil from Fischer-Tropsch wax, which synthesis method comprises: (a) separating the Fischer-Tropsch synthesis product into a fraction (i) having a boiling point in the middle distillate oil range and lower, a heavy tail fraction (iii), and an intermediate base oil precursor fraction (ii) having a boiling point between fraction (i) and fraction (iii); (b) subjecting the base oil precursor fraction (ii) to a catalytic hydroisomerization and catalytic dewaxing process to produce one or more base oil grades; (c) subjecting the heavy tail fraction (iii) to a conversion step to produce a fraction (iv) having a lower boiling point than the heavy tail fraction (iii); and (d) subjecting the high boiling point fraction (v) of fraction (iv) to a catalytic hydroisomerization and catalytic dewaxing process to produce one or more base oil grades. This method can produce qualified lubricating base oil through multiple fractionation and hydrogenation conversion. However, the heavy tail oil fraction undergoes hydrogenation conversion, fractionation, catalytic hydrogenation isomerization and then catalytic dewaxing to produce base oil. The process is too complicated, which will result in a decrease in the yield of lubricating base oil and an increase in viscosity index loss.

[0006] CN107760375A discloses a method for converting heavy Fischer-Tropsch wax, which includes: distilling and separating the heavy Fischer-Tropsch wax; contacting the obtained second component with a weight percentage content of more than 90% of the fraction with a carbon number greater than 40 with a hydroconversion catalyst, and contacting the material obtained after the contact with the first component with a weight percentage content of more than 90% of the fraction with a carbon number less than or equal to 40, respectively or together with a hydrotreating catalyst; contacting the hydrotreated raw material with an isomerization decondensation catalyst; contacting the wax conversion product oil with a hydrorefining catalyst; and distilling and separating the hydrorefining product oil. Although the method has a relatively high yield for 6# base oil, the reaction pressure is high during the preparation process, the safety factor of the preparation process is low, and there is also a problem of a long process flow.

[0007] In summary, the above-mentioned different conversion methods for Fischer-Tropsch wax can obtain relatively high viscosity index lubricating base oil, but due to the wide distillation range of Fischer-Tropsch wax, its conversion process has many steps and complex reactions, which will lead to low base oil yield, and the product will have low isomerization degree of wax precipitation after standing for a period of time, and the appearance is not clear and bright, and the existing method cannot produce high-quality 4cSt and 6cSt base oil. In order to improve the yield and quality of lubricating base oil products, it is necessary to further develop the Fischer-Tropsch wax conversion process. Summary of the invention

[0008] The main purpose of the present invention is to provide a lubricating oil base oil and a preparation method thereof, so as to solve the problems in the prior art of synthesizing lubricating oil base oil, such as multiple conversion processing steps, complex reactions, low base oil yield and low quality, and inability to simultaneously produce high-quality 4 cSt base oil and 6 cSt base oil.

[0009] In order to solve the above problems, the present invention provides a lubricating oil base oil and a preparation method thereof, the preparation method comprising: subjecting Fischer-Tropsch wax with a distillation range of 400 to 550° C. to a hydroisomerization reaction under the action of a hydroisomerization catalyst, and then subjecting the lubricating oil base oil to a hydrorefining reaction and distillation under the action of a hydrorefining catalyst; wherein the preparation method of the hydrorefining catalyst comprises the following steps: step (1), mixing an alkali, an aluminum source, a template, a silicon source and water to form a mixed solution, subjecting the mixed solution to a crystallization reaction to obtain a reaction solution A; step (2), cooling, filtering and quenching the reaction solution A; washing, first drying and first calcining to obtain ZSM-48 seed crystals; step (3), preparing ZSM-48 molecular sieve according to the preparation method of step (1) and step (2), and adding ZSM-48 seed crystals when preparing the mixed solution; step (4), subjecting the ZSM-48 molecular sieve to ammonium exchange and second calcination to obtain an active ZSM-48 molecular sieve; step (5), mixing the active ZSM-48 molecular sieve with a binder and molding to obtain a molded carrier; step (6), loading the molded carrier with noble metal ions, and then subjecting the molded carrier to second drying and third calcination to obtain a hydroisomerization catalyst.

[0010] Furthermore, the saturated hydrocarbon content of the Fischer-Tropsch wax is ≥90%; preferably, the concentration of the seed crystals in the crystallization reaction system formed in step (3) is 2000-5000 ppm.

[0011] Furthermore, the ammonium exchange process comprises: treating the ZSM-48 molecular sieve with ammonia water or a salt containing ammonium ions; preferably, the salt containing ammonium ions is ammonium nitrate.

[0012] Preferably, the crystallization is a one-stage crystallization or a segmented crystallization; preferably, the temperature of the one-stage crystallization is 160-180°C; preferably, the segmented crystallization temperature is 100-180°C; preferably, the crystallization time is 20-48h; preferably, the segmented crystallization is a two-stage crystallization performed sequentially, in which the first stage crystallization temperature is less than the second stage crystallization temperature, and the difference between the first stage crystallization temperature and the second stage crystallization temperature is 40-80°C; preferably, in the segmented crystallization, the time of the first stage crystallization is 8-20h, and the time of the second stage crystallization is 12-33h.

[0013] Furthermore, the silicon-aluminum ratio of the ZSM-48 molecular sieve is 70 to 180; preferably, the specific surface area of ​​the ZSM-48 molecular sieve is 200 to 250 m 2 / g, preferably, the weight ratio of ZSM-48 molecular sieve and binder in the shaped carrier is (65-75)%:(25-35)%; preferably, the binder is SB powder; preferably, the ZSM-48 molecular sieve is a rod-like structure; preferably, the axial size of the ZSM-48 molecular sieve is 0.5-5μm, and the radial size is 300-1000nm.

[0014] Furthermore, in step (5), the process of loading the shaped carrier with the precious metal ions is to immerse the shaped carrier in a solution containing precious metal ions once or in batches; preferably, the loading amount of the precious metal ions is 0.3-0.5%; preferably, when loading in batches, the first loading amount is 0.1-0.3%, and the second loading amount is 0.1-0.2%; preferably, the precious metal is Pt and / or Pd; preferably, the Pt source is one or more of chloroplatinic acid, tetraammineplatinum dichloride and tetraammineplatinum dinitrate; preferably, the Pd source is palladium chloride.

[0015] Furthermore, the weak acid content of the hydroisomerization catalyst is 0.20 to 0.35 mmol / g, and the medium-strong acid content is 0.10 to 0.25 mmol / g; preferably, the specific surface area of ​​the hydroisomerization catalyst is 200 to 250 m 2 ·g -1 .

[0016] Furthermore, the temperature of the hydroisomerization reaction is 300-380°C, the hydrogen partial pressure is 2-10 MPa, and the volume space velocity is 0.3-2 h -1 , the hydrogen-oil volume ratio is (200-2000):1; preferably, the temperature of the hydroisomerization reaction is 310-360°C, the hydrogen partial pressure is 3-8 MPa, and the volume space velocity is 0.5-1.5 h -1 , the volume ratio of hydrogen to oil is (500~1500):1.

[0017] Furthermore, the temperature of the hydrofining reaction is 200-280°C, and the volume space velocity is 0.2-2h -1 , the hydrogen-oil volume ratio is (200-2000):1, the hydrogen partial pressure is 2-10 MPa; preferably, the temperature of the hydrofining reaction is 220-260°C, and the volume space velocity is 0.5-1.6 h -1 , the volume ratio of hydrogen to oil is (500-1500):1, and the hydrogen partial pressure is 3-8 MPa; preferably, the hydrorefining catalyst comprises an active metal and a carrier loaded with the active metal, wherein the active metal is one or more of Pt, Pd, Ni and W, and the carrier is at least one of macroporous alumina and silica-alumina; preferably, the active metal is Pt and / or Pd; preferably, the carrier is macroporous alumina; preferably, the loading amount of the active metal in the hydrorefining catalyst is 0.3-0.5%.

[0018] According to another aspect of the present invention, a lubricating oil base oil is also provided. The lubricating oil base oil is prepared by the above-mentioned preparation method, and the lubricating oil base oil includes a 2cSt base oil with a distillation range of 260-370°C, a 3cSt base oil with a distillation range of 370-400°C, a 4cSt base oil with a distillation range of 400-450°C, and a 6cSt base oil with a distillation range of above 450°C.

[0019] The invention provides a lubricating oil base oil and a preparation method thereof. In the method for preparing the lubricating oil base oil, a hydroisomerization catalyst is synthesized, and the synthesized hydroisomerization catalyst has a good matching effect on Fischer-Tropsch wax with a distillation range of 400-550° C. and shows high isomerization selectivity for the Fischer-Tropsch wax. The Fischer-Tropsch wax with a distillation range of 400-550° C. is subjected to the hydroisomerization catalyst prepared by the invention to prepare a lubricating oil base oil with a high viscosity index, a low pour point and a low cloud point. The method for preparing the lubricating oil base oil also has the advantages of high yield and simple preparation process flow. At the same time, the preparation method can also simultaneously produce 4cSt base oil and 6cSt base oil with relatively high quality. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] The drawings constituting a part of the present application are used to provide a further understanding of the present invention. The exemplary embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation of the present invention. In the drawings:

[0021] Figure 1 The schematic diagram of the process flow of preparing lubricating oil base oil according to the present invention is shown;

[0022] Figure 2 The XRD spectrum of the ZSM-48 molecular sieve prepared in Example 1 of the present invention is shown;

[0023] Figure 3 The SEM spectrum of the ZSM-48 molecular sieve prepared in Example 1 of the present invention is shown. DETAILED DESCRIPTION

[0024] It should be noted that, in the absence of conflict, the embodiments and features in the embodiments of the present application can be combined with each other. The present invention will be described in detail below with reference to the accompanying drawings and in combination with the embodiments.

[0025] As described in the background technology section, in the prior art, in the process of synthesizing lubricating oil base oil using Fischer-Tropsch wax, due to the wide distillation range of Fischer-Tropsch wax, the conversion process steps are many and the reaction is complicated, which will lead to a low yield of base oil. In addition, after the prepared base oil product is left to stand for a period of time, wax with a low degree of isomerization will precipitate, the appearance is not clear and bright, and the quality is low. In addition, the existing base oil preparation method cannot simultaneously produce 4cSt and 6cSt base oils with high quality.

[0026] In order to solve the above problems, the present invention provides a method for preparing a lubricating oil base oil, which comprises subjecting a Fischer-Tropsch wax having a distillation range of 400 to 550° C. to a hydroisomerization reaction under the action of a hydroisomerization catalyst, and then subjecting the Fischer-Tropsch wax to a hydroisomerization reaction under the action of a hydrorefining catalyst and distillation to obtain the lubricating oil base oil; wherein the method for preparing the hydroisomerization catalyst comprises the following steps: step (1), mixing an alkali, an aluminum source, a template, a silicon source and water to form a mixed solution, and subjecting the mixed solution to a crystallization reaction to obtain a reaction solution A; step (2), cooling, filtering, washing and purifying the reaction solution A; The invention further comprises the steps of: washing, first drying and first calcining to obtain ZSM-48 seed crystals; step (3), preparing ZSM-48 molecular sieve according to the preparation method of step (1) and step (2), and adding ZSM-48 seed crystals when preparing the mixed solution; step (4), subjecting the ZSM-48 molecular sieve to ammonium exchange and second calcination to obtain an active ZSM-48 molecular sieve; step (5), mixing the active ZSM-48 molecular sieve with a binder and molding to obtain a molded carrier; step (6), loading the molded carrier with noble metal ions, and then subjecting the molded carrier to a second drying and a third calcination to obtain a hydroisomerization catalyst.

[0027] Specifically, in the preparation method of the synthetic lubricating oil base oil, a hydroisomerization catalyst for hydroisomerization reaction is first prepared, and then a Fischer-Tropsch wax with a distillation range of 400 to 550° C. is subjected to a hydroisomerization reaction under the action of the hydroisomerization catalyst, and finally a lubricating oil base oil is obtained by hydrorefining reaction and distillation separation under the action of a hydrorefining catalyst (the process flow diagram is shown in FIG. Figure 1 shown).

[0028] In the preparation process of the above-mentioned hydroisomerization catalyst, alkali, aluminum source, template, silicon source and water are first mixed to carry out crystallization reaction, and then the reaction solution is cooled, filtered, washed, dried and first roasted to obtain ZSM-48 seed crystals, and then the ZSM-48 molecular sieve is prepared according to the preparation method of step (1) and step (2), and the ZSM-48 seed crystals prepared in step (2) are added when preparing the mixed solution. Adding seed crystals when preparing ZSM-48 molecular sieve can make the synthesized molecular sieve have higher crystallinity, and better specific surface area and mesoporous pore volume, which is conducive to improving the activity and selectivity of the catalyst, thereby further improving the quality of the prepared lubricating oil base oil. In addition, adding homemade seed crystals when preparing ZSM-48 molecular sieve can make the specific surface area, weak acid amount and medium-strong acid amount of the obtained hydroisomerization catalyst more suitable, and can also shorten the crystallization time, effectively controlling the preparation cost of the hydroisomerization catalyst and the time cost of production. The prepared ZSM-48 molecular sieve is subjected to ammonium exchange and calcination to reduce the alkali metal content in the ZSM-48 molecular sieve, and the obtained active ZSM-48 molecular sieve has better acid sites. After the noble metal ions and the molecular sieve are loaded, the metal sites can have better matching with the acid sites, further improving the selectivity of the prepared hydroisomerization catalyst for Fischer-Tropsch wax with a distillation range of 400 to 550°C. Finally, the active ZSM-48 molecular sieve is mixed with a binder and molded, and the molded carrier is loaded with noble metal ions, and then dried and thirdly calcined to obtain a hydroisomerization catalyst.

[0029] The present invention uses Fischer-Tropsch wax with a distillation range of 400 to 550° C. as a raw material for producing lubricating base oil, and synthesizes a hydroisomerization catalyst with high isomerization selectivity for the Fischer-Tropsch wax in this distillation range. Under the action of the prepared hydroisomerization catalyst, the prepared lubricating base oil can have a high viscosity index, a low pour point, a low cloud point, and a high quality. This method not only improves the quality of the product, but also further reduces the catalyst production cost, with significant economic and environmental benefits. In addition, the lubricating base oil prepared by this method has good thermal stability and antioxidant properties, and is suitable for various high-performance lubrication needs.

[0030] It should be further explained here that, in addition to ZSM-48 molecular sieve, other common one-dimensional medium-pore ten-membered ring molecular sieves can also be used as carriers for preparing the hydroisomerization catalyst of the present invention, which also has good effects.

[0031] In the process of synthesizing seed crystals and synthesizing ZSM-48 molecular sieves, the addition ratio of alkali, aluminum source, template, aluminum source and water can be adjusted according to actual needs. Preferably, the ratio of the molar amount of alkali to the molar amount of silicon in the silicon source is 0.06-0.20, the ratio of the molar amount of template to the molar amount of silicon in the silicon source is 0.015-0.030, the ratio of the molar amount of water to the molar amount of silicon in the silicon source is 15-30, and the addition ratio of silicon source and aluminum source can be further adjusted according to the specific silicon-aluminum ratio requirements. The first drying temperature, first drying time, first calcination temperature and first calcination time involved in the preparation of seed crystals and molecular sieves of the present invention are not specifically limited, and can be adjusted as needed in the actual preparation process. Preferably, the first drying temperature is 80-120°C, and the first drying time is 4-10h; the first calcination temperature is 500-600°C, and the first calcination time is 6-10h. The second calcination temperature when preparing the active ZSM-48 molecular sieve is preferably 500-600°C, and the second calcination time is 6-10h. After the shaped carrier is loaded with the noble metal ions, the second drying temperature is preferably 60-120°C, the second drying time is 4-6h, the third calcination temperature is 400-600°C, and the second calcination time is 2-6h. In the process of preparing the molecular sieve, no special requirements are made for the alkali, aluminum source, template and aluminum source. Preferably, the alkali can be selected from sodium hydroxide and potassium hydroxide; the aluminum source can be selected from sodium aluminate and pseudo-boehmite; the template can be selected from hexamethylammonium bromide and 1,6-hexanediamine; the silicon source can be selected from silica sol, sodium silicate and fumed silica.

[0032] In a preferred embodiment, the saturated hydrocarbon content of the Fischer-Tropsch wax is ≥ 90%. Fischer-Tropsch wax with a high saturated hydrocarbon content can improve the stability of the final product and reduce the generation of volatile substances. Controlling the saturated hydrocarbon content of the Fischer-Tropsch wax within the above range can make the obtained lubricating base oil of better quality. Preferably, the concentration of the seed in the crystallization reaction system formed in step (3) is 2000-5000ppm. In particular, after a large number of experiments, the inventor creatively found that the method for preparing a hydroisomerization catalyst according to the present invention can control the amount of seed added within the above range, that is, the obtained hydroisomerization catalyst can have an excellent catalytic effect. This is because the addition of seed during the crystallization reaction helps to form microcrystalline nuclei in the early stage, and the presence of a small amount of microcrystalline nuclei can further promote the crystallinity. When the number of crystal nuclei reaches a certain value, continuing to increase the amount of seed, the crystallinity in the system cannot be further promoted. On the contrary, excessively increasing the amount of seed added will cause a certain degree of crystal aggregation during the crystallization process, affecting the crystallinity, and then affecting the catalytic performance of the catalyst. On the other hand, adding too much seed crystals will cause unnecessary waste and increase the preparation cost of the catalyst.

[0033] In a preferred embodiment, the ammonium exchange process includes: treating the ZSM-48 molecular sieve with ammonia water or a salt containing ammonium ions; preferably, the salt containing ammonium ions is ammonium nitrate. The ammonium exchange process can effectively remove alkali metal ions in the molecular sieve, improve the acidity of the molecular sieve, and thus enhance the activity of the catalyst. In the present invention, ammonia water or ammonium ions are used to treat the ZSM-48 molecular sieve, which can not only effectively remove sodium ions in the molecular sieve, but also make the molecular sieve at a suitable acidity, which can effectively reduce the number of ammonium exchanges. The ZSM-48 molecular sieve treated with ammonium exchange shows higher catalytic efficiency in the hydroisomerization reaction and is suitable for the production of high-quality lubricating oil base oil. Preferably, in the process of ammonium exchange, the concentration of ammonia water is preferably controlled to be 0.5-10 mol / L, and the concentration of the salt containing ammonium ions is controlled to be 1-5 mol / L. Preferably, the number of ammonium exchanges is 1-3 times.

[0034] Preferably, before the ammonium exchange, the process further includes: stirring the ZSM-48 molecular sieve in an alkaline solution at 60-80° C. for 2-5 hours. By way of example but not limitation, the alkaline solution used in the process is at least one of ammonia water, sodium bicarbonate, sodium carbonate and sodium hydroxide solution, and the concentration of the alkaline solution is 0.1-1 mol / L. The pretreatment operation before the ammonium exchange can make the ammonium exchange effect better.

[0035] In a preferred embodiment, the crystallization is one-stage crystallization or segmented crystallization; preferably, the temperature of one-stage crystallization is 160-180°C; preferably, the segmented crystallization temperature is 100-180°C; preferably, the crystallization time is 20-48h, and when the crystallization temperature and the crystallization time are within the above range, a molecular sieve with good crystallinity can be obtained. Preferably, the segmented crystallization is two-stage crystallization carried out in sequence, and the crystallization temperature of the first stage in the two-stage crystallization is less than the crystallization temperature of the second stage, and the difference between the crystallization temperature of the first stage and the crystallization temperature of the second stage is 40-80°C; preferably, the time of the first stage crystallization in the segmented crystallization is 8-20h, and the time of the second stage crystallization is 12-28h. Segmented crystallization can better control the crystallization process of the molecular sieve, improve the crystallinity and structural stability of the molecular sieve, and thus improve the performance of the catalyst. The segmented crystallization method can effectively shorten the high-temperature crystallization time and the total crystallization time. Especially in large-scale industrial production processes, the use of the segmented crystallization method can ensure the consistency and stability of the catalyst and achieve the purpose of effective cost savings.

[0036] In a preferred embodiment, the silicon-aluminum ratio of the ZSM-48 molecular sieve is 70 to 180, and the specific surface area of ​​the ZSM-48 molecular sieve is 200 to 250 m 2 / g. Controlling the molar ratio of silicon dioxide and aluminum oxide and the specific surface area in the prepared ZSM-48 molecular sieve within the above range can provide more active sites for the ZSM-48 molecular sieve, further improving the catalytic efficiency of the catalyst. Preferably, the weight ratio of ZSM-48 molecular sieve and binder in the molded carrier is (65-75)%: (25-35)%; preferably, the binder is SB powder; preferably, the ZSM-48 molecular sieve is a rod-shaped structure; preferably, the axial size of the ZSM-48 molecular sieve is 0.5-5μm, and the radial size is 300-1000nm. Molding the carrier is beneficial to the subsequent metal loading process. Controlling the ZSM-48 molecular sieve to be a rod-shaped structure and controlling the size of the molecular sieve within the above range can make the obtained molecular sieve have better mass transfer performance and is suitable for high-throughput industrial production processes.

[0037] In a preferred embodiment, the process of loading the shaped carrier with the noble metal ions in step (5) is: immersing the shaped carrier in a solution containing noble metal ions in a single or divided manner; preferably, the loading amount of the noble metal ions is 0.3-0.5%. By controlling the loading amount of the noble metal ions in the active molecular sieve shaped carrier to 0.3-0.5%, the catalyst can have a suitable catalytic activity while avoiding the problem of excessive cost caused by excessive use of noble metals. Preferably, when loading in batches, the first loading amount is 0.1-0.3%, and the second loading amount is 0.1-0.2%; preferably, the noble metal is Pt and / or Pd; preferably, the Pt source is one or more of chloroplatinic acid, dichlorotetraamineplatinum and dinitratetetraamineplatinum; preferably, the Pd source is palladium chloride. The method of loading in batches can distribute the noble metal ions more evenly, thereby further improving the stability and service life of the catalyst, and is suitable for industrial production processes that run continuously for a long time.

[0038] In a preferred embodiment, the weak acid content of the hydroisomerization catalyst is 0.20 to 0.35 mmol / g, and the medium-strong acid content is 0.10 to 0.25 mmol / g; preferably, the specific surface area of ​​the hydroisomerization catalyst is 200 to 250 m 2 ·g -1 Controlling the amount of weak acid and medium-strong acid within the above range can effectively promote the hydrogenation isomerization reaction, improve the isomerization selectivity of the catalyst catalytic reaction and improve the conversion rate of the catalytic isomerization reaction; at the same time, controlling the specific surface area of ​​the catalyst within the above range can provide more active sites, which is beneficial to improving the catalytic efficiency and producing high-quality lubricant base oil.

[0039] In a preferred embodiment, the temperature of the hydroisomerization reaction is 300-380°C, the hydrogen partial pressure is 2-10 MPa, and the volume space velocity is 0.3-2 h -1, the volume ratio of hydrogen to oil is (200-2000):1; controlling the hydroisomerization reaction conditions within the above range can ensure the efficient hydroisomerization reaction, improve the conversion rate and selectivity of Fischer-Tropsch wax, and thus prepare high-purity and high-performance lubricant base oil. Suitable for the lubrication needs of various high-performance engines and industrial equipment. Preferably, the temperature of the hydroisomerization reaction is 310-360°C, the hydrogen partial pressure is 3-8MPa, and the volume space velocity is 0.5-1.5h -1 , the volume ratio of hydrogen to oil is (500~1500):1.

[0040] In a preferred embodiment, the temperature of the hydrofining reaction is 200-280°C, and the volume space velocity is 0.2-2h -1 , the hydrogen-oil volume ratio is (200-2000):1, and the hydrogen partial pressure is 2-10 MPa; controlling the conditions of the hydrofining reaction within the above range can effectively remove impurities in the lubricating oil base oil and improve its purity and stability. Preferably, the temperature of the hydrofining reaction is 220-260°C, and the volume space velocity is 0.5-1.6h -1 , the volume ratio of hydrogen to oil is (500-1500):1, and the hydrogen partial pressure is 3-8MPa. Preferably, the hydrorefining catalyst includes an active metal and a carrier loaded with the active metal, wherein the active metal is one or more of Pt, Pd, Ni and W, and the carrier is at least one of macroporous alumina and silicon aluminum oxide; preferably, the active metal is Pt and / or Pd; preferably, the carrier is macroporous alumina; preferably, the loading amount of the active metal in the hydrorefining catalyst is 0.3-0.5%. Controlling the composition of the hydrorefining reaction catalyst within the above range can further improve the purity of the hydrorefining reaction, which is conducive to the production of high-quality lubricating oil base oil. The hydrorefining catalyst can be purchased commercially or made by yourself, and the carrier molding method is similar to the molecular sieve molding method when preparing the hydroisomerization catalyst of the present invention, which will not be described in detail here. The pore size of the macroporous alumina carrier in the hydrorefining catalyst is between 50nm and 1μm, and the carrier has the advantages of high specific surface area and good pore structure.

[0041] In the actual preparation process, the hydrogen partial pressure of the hydroisomerization reaction and the hydrofining reaction process can be controlled to be consistent, which can be beneficial to energy saving and reduce production costs. It is worth mentioning that by using the hydroisomerization catalyst proposed in the present invention, the hydrogen partial pressure is controlled within the above range, and even if the pressure is relatively low, a good yield can be achieved without deliberately increasing the reaction pressure. It is further explained that the hydroisomerization catalyst prepared by the present invention has good compatibility with the Fischer-Tropsch wax with a distillation range of 400 to 550°C.

[0042] According to another aspect of the present invention, a lubricating base oil is also provided, which is prepared by the above-mentioned preparation method, and the lubricating base oil includes a 2cSt base oil with a fraction of 260-370°C, a 3cSt base oil with a fraction of 370-400°C, a 4cSt base oil with a fraction of 400-450°C, and a 6cSt base oil with a fraction of more than 450°C. The preparation method of the lubricating base oil of the present invention can simultaneously produce 3cSt base oil, 4cSt base oil and 6cSt base oil in the process of vacuum distillation, and has the advantages of high viscosity index, low pour point, low cloud point, etc. In addition, in the preparation method of the present invention, naphtha with a fraction of <160°C and a light white oil fraction with a fraction of 160-260°C can also be obtained in the process of atmospheric distillation.

[0043] The present application is further described in detail below in conjunction with specific embodiments. These embodiments should not be construed as limiting the scope of protection claimed in the present application.

[0044] It should be further explained here that the Fischer-Tropsch wax with a distillation range of 400-550°C used in the embodiments of the present invention and the comparative examples is from the same batch, the hydrorefining catalyst used in the present invention can be self-made or purchased, and the ones used in the embodiments of the present invention are all self-made, with macroporous alumina as the carrier, and are realized by impregnating a corresponding amount of active metal ions, wherein the active metal loading in the Pt-type hydrorefining catalyst used is 0.4%, and the active metal loading in the Pt / Pd-type hydrorefining catalyst is 0.3%. The alkali source involved in the embodiments and the comparative examples is sodium hydroxide, the aluminum source is sodium aluminate, the template agent is hexamethylammonium bromide, and the silicon source is silica sol.

[0045] Example 1

[0046] (1) Synthetic seed crystals

[0047] Take 1.2g of sodium hydroxide, 0.4g of sodium aluminate, 2g of template, 60g of silica sol and 60g of water, mix and stir evenly, and place in a crystallization kettle for staged crystallization, wherein the temperature of the first stage of crystallization is 110℃, the time is 16h, and the temperature of the second stage of crystallization is 175℃, the time is 20h. After the crystallization is completed, the ZSM-48 seed crystal is obtained by cooling, filtration, washing, drying and roasting. Among them, the washing solvent is water, the drying temperature is 100℃, the time is 6h, and the roasting temperature is 600℃, the time is 8h.

[0048] (2) Preparation of active molecular sieves

[0049] 0.8g of sodium hydroxide, 0.65g of sodium aluminate, 2.1g of template, 60g of silica sol, 60g of water and seed crystals were mixed and stirred evenly and then placed in a crystallization kettle for crystallization, wherein the concentration of seed crystals in the above crystallization system is 2000ppm, the crystallization temperature is 180℃, and the time is 30h. After the crystallization is completed, the ZSM-48 molecular sieve is obtained by cooling, filtration, washing, drying and roasting, wherein the washing solvent is water, the drying temperature is 120℃, the time is 4h, the roasting temperature is 500℃, the time is 10h, the silicon-aluminum ratio of the molecular sieve is 90, the axial size of the molecular sieve is 2.5-3.0μm, and the radial size is 600-800nm. The prepared ZSM-48 molecular sieve was subjected to XRD test and SEM test. The XRD spectrum of the ZSM-48 molecular sieve is as shown in the figure Figure 2 As shown, the SEM spectrum of ZSM-48 molecular sieve is as follows Figure 3 As shown. Figure 2 The XRD spectrum in the figure shows that the synthesized ZSM-48 molecular sieve is pure phase and has a high relative crystallinity. Figure 3 The SEM spectrum in the figure shows that the prepared ZSM-48 molecular sieve is a rod-like structure with a relatively uniform structure, with a long axis of 1.2 to 1.6 μm and a short axis of 600 to 700 nm. The prepared ZSM-48 molecular sieve has the characteristics of uniform structure, which is conducive to better loading of active metal ions, so that the prepared hydroisomerization catalyst can exert better catalytic performance.

[0050] Then, the prepared ZSM-48 molecular sieve was ion exchanged three times in 1 mol / L ammonium nitrate solution and calcined at 550° C. for 10 h to obtain an active ZSM-48 molecular sieve.

[0051] (3) Preparation of Hydroisomerization Catalyst

[0052] The active ZSM-48 molecular sieve prepared above was mixed with SB powder in a weight ratio of 65%:35%, and a shaped carrier was prepared by the kneading-extrusion method. The carrier was then immersed in a tetraammineplatinum dichloride solution, dried at 60°C for 4 hours, and calcined at 400°C for 4 hours to obtain a hydroisomerization catalyst with a metal Pt loading of 0.50%. The test results of the obtained hydroisomerization catalyst are shown in Table 16.

[0053] (4) Preparation of lubricating oil base oil

[0054] The Fischer-Tropsch wax with a distillation range of 400-550°C is used as a raw material, and a hydroisomerization reaction is carried out under the action of the hydroisomerization catalyst prepared above, and a hydrorefining reaction is carried out under the action of a hydrorefining catalyst with Pt as an active metal and macroporous alumina as a carrier. The temperature of the hydroisomerization reaction is 340°C, the hydrogen partial pressure is 3MPa, and the volume space velocity is 1.0h -1, the hydrogen-oil volume ratio is 800:1; the temperature of the hydrotreating reaction is 240°C, and the volume space velocity is 1.0h -1 , the hydrogen-oil volume ratio is 800:1, and the hydrogen partial pressure is 3MPa. The obtained hydrorefined product is separated under atmospheric distillation conditions to obtain naphtha with a fraction less than 160°C and a light white oil fraction with a fraction of 160-260°C, and under reduced pressure distillation conditions to obtain lubricating oil base oils, including 2cSt base oil with a fraction of 260-370°C, 3cSt base oil with a fraction of 370-400°C, 4cSt base oil with a fraction of 400-450°C, and 6cSt base oil with a fraction of more than 450°C. The test data of the obtained base oils are shown in Table 1.

[0055] Table 1

[0056]

[0057] Example 2

[0058] (1) Synthetic seed crystals

[0059] The seed crystals prepared in Example 1 were used as seed crystals for preparing ZSM-48 molecular sieve in this example.

[0060] (2) Preparation of active molecular sieves

[0061] 1.4 g of sodium hydroxide, 0.55 g of sodium aluminate, 2.1 g of template, 60 g of silica sol, 65 g of water and seed crystals were mixed and stirred evenly, and then placed in a crystallization kettle for staged crystallization, wherein the concentration of seed crystals in the above crystallization system is 3000 ppm, the temperature of the first stage of crystallization is 100°C, the time is 12 h, the temperature of the second stage of crystallization is 170°C, and the time is 24 h. After the crystallization is completed, the ZSM-48 molecular sieve is obtained by cooling, filtering, washing, drying and calcining, wherein the washing solvent is water, the drying temperature is 120°C, the time is 4 h, the calcination temperature is 550°C, the time is 10 h, the silicon-aluminum ratio of the molecular sieve is 110, the axial size of the molecular sieve is 2.0-2.5 μm, and the radial size is 550-700 nm. Then, the prepared ZSM-48 molecular sieve was ion exchanged three times in 1 mol / L ammonium nitrate solution and calcined at 550° C. for 6 h to obtain an active ZSM-48 molecular sieve.

[0062] (3) Preparation of Hydroisomerization Catalyst

[0063] The active ZSM-48 molecular sieve prepared above was mixed with SB powder in a weight ratio of 70%:30%, and a shaped carrier was prepared by the kneading-extrusion method. It was then immersed in a tetraammineplatinum dichloride solution, dried at 60°C for 4 hours, and calcined at 400°C for 4 hours to obtain a hydroisomerization catalyst with a metal Pt loading of 0.45%. The test results of the obtained hydroisomerization catalyst are shown in Table 16.

[0064] (4) Preparation of lubricating oil base oil

[0065] The Fischer-Tropsch wax with a distillation range of 400-550°C is used as a raw material, and a hydroisomerization reaction is carried out under the action of the hydroisomerization catalyst prepared above, and a hydrorefining reaction is carried out under the action of a hydrorefining catalyst with Pt / Pd as an active metal and macroporous alumina as a carrier. The temperature of the hydroisomerization reaction is 335°C, the hydrogen partial pressure is 3.5MPa, and the volume space velocity is 0.8h -1 , the hydrogen-oil volume ratio is 600:1; the temperature of the hydrotreating reaction is 240°C, and the volume space velocity is 0.8h -1 , the hydrogen-oil volume ratio is 600:1, and the hydrogen partial pressure is 3.5MPa. The obtained hydrorefined product is separated under atmospheric distillation conditions to obtain naphtha with a fraction less than 160°C and a light white oil fraction with a fraction of 160-260°C, and under reduced pressure distillation conditions to obtain lubricating oil base oils, including 2cSt base oil with a fraction of 260-370°C, 3cSt base oil with a fraction of 370-400°C, 4cSt base oil with a fraction of 400-450°C, and 6cSt base oil with a fraction of more than 450°C. The test data of the obtained base oils are shown in Table 2.

[0066] Table 2

[0067]

[0068] Example 3

[0069] (1) Synthetic seed crystals

[0070] The seed crystals prepared in Example 1 were used as seed crystals for preparing ZSM-48 molecular sieve in this example.

[0071] (2) Preparation of active molecular sieves

[0072] 0.9 g of sodium hydroxide, 0.45 g of sodium aluminate, 2.1 g of template, 60 g of silica sol, 65 g of water and seed crystals were mixed and stirred evenly, and then placed in a crystallization kettle for staged crystallization, wherein the concentration of seed crystals in the above crystallization system is 4000 ppm, the temperature of the first stage of crystallization is 100°C, the time is 20 h, the temperature of the second stage of crystallization is 180°C, and the time is 12 h. After the crystallization is completed, the ZSM-48 molecular sieve is obtained by cooling, filtering, washing, drying and calcining, wherein the washing solvent is water, the drying temperature is 80°C, the time is 8 h, the calcination temperature is 550°C, the time is 8 h, the silicon-aluminum ratio of the molecular sieve is 130, the axial size of the molecular sieve is 1.5-2.0 μm, and the radial size is 500-650 nm. The prepared ZSM-48 molecular sieve was then stirred in 0.1 mol / L ammonia water at 60°C for 2 hours, dried, ion exchanged twice in 1 mol / L ammonium nitrate solution, and calcined at 550°C for 6 hours to obtain an active ZSM-48 molecular sieve.

[0073] (3) Preparation of Hydroisomerization Catalyst

[0074] The active ZSM-48 molecular sieve prepared above was mixed with SB powder in a weight ratio of 70%:30%, and a shaped carrier was prepared by the kneading-extrusion method. The carrier was then placed in a tetraammine dinitrate platinum solution for loading and impregnation in batches, with the first loading amount being 0.25% and the second loading amount being 0.15%. The carrier was then dried at 60°C for 6 hours and calcined at 400°C for 2 hours to obtain a hydroisomerization catalyst with a metal Pt loading amount of 0.40%. The test results of the obtained hydroisomerization catalyst are shown in Table 16.

[0075] (4) Preparation of lubricating oil base oil

[0076] The Fischer-Tropsch wax with a distillation range of 400-550°C is used as a raw material, and a hydroisomerization reaction is carried out under the action of the hydroisomerization catalyst prepared above, and a hydrorefining reaction is carried out under the action of a hydrorefining catalyst with Pt as an active metal and macroporous alumina as a carrier. The temperature of the hydroisomerization reaction is 330°C, the hydrogen partial pressure is 3MPa, and the volume space velocity is 0.6h -1 , the hydrogen-oil volume ratio is 600:1; the temperature of the hydrotreating reaction is 240°C, and the volume space velocity is 0.6h -1, the hydrogen-oil volume ratio is 600:1, and the hydrogen partial pressure is 3MPa. The obtained hydrorefined product is separated under atmospheric distillation conditions to obtain naphtha with a fraction less than 160°C and a light white oil fraction with a fraction of 160-260°C, and under reduced pressure distillation conditions to obtain lubricating oil base oils, including 2cSt base oil with a fraction of 260-370°C, 3cSt base oil with a fraction of 370-400°C, 4cSt base oil with a fraction of 400-450°C, and 6cSt base oil with a fraction of more than 450°C. The test data of the obtained base oils are shown in Table 3.

[0077] Table 3

[0078]

[0079]

[0080] Example 4

[0081] (1) Synthetic seed crystals

[0082] The seed crystals prepared in Example 1 were used as seed crystals for preparing ZSM-48 molecular sieve in this example.

[0083] (2) Preparation of active molecular sieves

[0084] 1.0 g of sodium hydroxide, 0.4 g of sodium aluminate, 2.1 g of template, 60 g of silica sol, 65 g of water and seed crystals were mixed and stirred evenly, and then placed in a crystallization kettle for staged crystallization, wherein the concentration of seed crystals in the above crystallization system is 5000 ppm, the temperature of the first stage of crystallization is 110°C, the time is 12 h, the temperature of the second stage of crystallization is 170°C, and the time is 20 h. After the crystallization is completed, the ZSM-48 molecular sieve is obtained by cooling, filtering, washing, drying and calcining, wherein the washing solvent is water, the drying temperature is 100°C, the time is 6 h, the calcination temperature is 550°C, the time is 8 h, the silicon-aluminum ratio of the molecular sieve is 150, the axial size of the molecular sieve is 1.5-2.0 μm, and the radial size is 500-650 nm. The prepared ZSM-48 molecular sieve was then stirred in 0.2 mol / L sodium bicarbonate at 70°C for 2 h, dried, ion exchanged once in 1 mol / L ammonium nitrate solution, and calcined at 550°C for 6 h to obtain an active ZSM-48 molecular sieve.

[0085] (3) Preparation of Hydroisomerization Catalyst

[0086] The active ZSM-48 molecular sieve prepared above was mixed with SB powder in a weight ratio of 75%:25%, and a shaped carrier was prepared by the kneading-extrusion method. The carrier was then placed in a chloroplatinic acid solution for loading and impregnation in batches, with the first loading amount being 0.2% and the second loading amount being 0.15%. After drying and calcining at 450°C for 4 hours, a hydroisomerization catalyst with a metal Pt loading amount of 0.35% was obtained. The test results of the obtained hydroisomerization catalyst are shown in Table 16.

[0087] (4) Preparation of lubricating oil base oil

[0088] The Fischer-Tropsch wax with a distillation range of 400-550°C is used as a raw material, and a hydroisomerization reaction is carried out under the action of the hydroisomerization catalyst prepared above, and a hydrorefining reaction is carried out under the action of a hydrorefining catalyst with Pt as an active metal and macroporous alumina as a carrier. The temperature of the hydroisomerization reaction is 337°C, the hydrogen partial pressure is 3.5MPa, and the volume space velocity is 0.7h -1 , the hydrogen-oil volume ratio is 800:1; the temperature of the hydrotreating reaction is 240°C, and the volume space velocity is 0.7h -1 , the hydrogen-oil volume ratio is 800:1, and the hydrogen partial pressure is 3.5MPa. The obtained hydrorefined product is separated under atmospheric distillation conditions to obtain naphtha with a fraction less than 160°C and a light white oil fraction with a fraction of 160-260°C, and under reduced pressure distillation conditions to obtain lubricating oil base oils, including 2cSt base oil with a fraction of 260-370°C, 3cSt base oil with a fraction of 370-400°C, 4cSt base oil with a fraction of 400-450°C, and 6cSt base oil with a fraction of more than 450°C. The test data of the obtained base oils are shown in Table 4.

[0089] Table 4

[0090]

[0091]

[0092] Example 5

[0093] (1) Synthetic seed crystals

[0094] The seed crystals prepared in Example 1 were used as seed crystals for preparing ZSM-48 molecular sieve in this example.

[0095] (2) Preparation of active molecular sieves

[0096] 0.9 g of sodium hydroxide, 0.35 g of sodium aluminate, 2.1 g of template, 60 g of silica sol, 65 g of water and seed crystals were mixed and stirred evenly, and then placed in a crystallization kettle for crystallization, wherein the concentration of seed crystals in the above crystallization system is 3000 ppm, the crystallization temperature is 170°C, and the time is 36 h. After the crystallization is completed, the ZSM-48 molecular sieve is obtained by cooling, filtering, washing, drying and roasting, wherein the washing solvent is water, the drying temperature is 120°C, the time is 4 h, the roasting temperature is 600°C, the time is 10 h, the silicon-aluminum ratio of the molecular sieve is 170, the axial size of the molecular sieve is 1.0-1.5 μm, and the radial size is 450-600 nm. The prepared ZSM-48 molecular sieve was then stirred in a 0.1 mol / L sodium hydroxide solution at 70°C for 2 h, dried, ion exchanged three times with a 1 mol / L ammonium nitrate solution, and calcined at 550°C for 8 h to obtain an active ZSM-48 molecular sieve.

[0097] (3) Preparation of Hydroisomerization Catalyst

[0098] The active ZSM-48 molecular sieve prepared above was mixed with SB powder in a weight ratio of 75%:25%, and a shaped carrier was prepared by the kneading-extrusion method. The carrier was then immersed in a tetraammineplatinum dichloride solution and dried and calcined at 400°C for 5 hours to obtain a hydroisomerization catalyst with a metal Pt loading of 0.30%. The test results of the obtained hydroisomerization catalyst are shown in Table 16.

[0099] (4) Preparation of lubricating oil base oil

[0100] The Fischer-Tropsch wax with a distillation range of 400-550°C is used as a raw material, and a hydroisomerization reaction is carried out under the action of the hydroisomerization catalyst prepared above, and a hydrorefining reaction is carried out under the action of a hydrorefining catalyst with Pt / Pd as an active metal and macroporous alumina as a carrier. The temperature of the hydroisomerization reaction is 339°C, the hydrogen partial pressure is 3.5MPa, and the volume space velocity is 0.8h -1 , the hydrogen-oil volume ratio is 800:1; the temperature of the hydrotreating reaction is 240°C, and the volume space velocity is 0.8h -1 , the hydrogen-oil volume ratio is 800:1, and the hydrogen partial pressure is 3.5MPa. The obtained hydrorefined product is separated under atmospheric distillation conditions to obtain naphtha with a fraction less than 160°C and a light white oil fraction with a fraction of 160-260°C, and under reduced pressure distillation conditions to obtain lubricating oil base oils, including 2cSt base oil with a fraction of 260-370°C, 3cSt base oil with a fraction of 370-400°C, 4cSt base oil with a fraction of 400-450°C, and 6cSt base oil with a fraction of more than 450°C. The test data of the obtained base oils are shown in Table 5.

[0101] Table 5

[0102]

[0103] Example 6

[0104] (1) Synthetic seed crystals

[0105] Take 1.2g of sodium hydroxide, 0.4g of sodium aluminate, 2g of template, 60g of silica sol and 60g of water, mix and stir evenly, and place in a crystallization kettle for staged crystallization, wherein the temperature of the first stage of crystallization is 100℃, the time is 20h, and the temperature of the second stage of crystallization is 170℃, the time is 12h. After the crystallization is completed, the ZSM-48 seed crystal is obtained by cooling, filtration, washing, drying and roasting. Among them, the washing solvent is water, the drying temperature is 80℃, the time is 10h, and the roasting temperature is 500℃, the time is 10h.

[0106] (2) Preparation of active molecular sieves

[0107] 0.9g of sodium hydroxide, 0.85g of sodium aluminate, 2.1g of template agent, 60g of silica sol and 65g of water and seed crystals were mixed and stirred evenly and then placed in a crystallization kettle for crystallization, wherein the concentration of seed crystals in the above crystallization system was 2000ppm, the crystallization temperature was 160℃, and the time was 48h. After the crystallization was completed, the ZSM-48 molecular sieve was obtained by cooling, filtration, washing, drying and roasting, wherein the washing solvent was water, the drying temperature was 120℃, the time was 4h, the roasting temperature was 600℃, the time was 6h, the silicon-aluminum ratio of the molecular sieve was 70, the axial size of the molecular sieve was 0.5-2μm, and the radial size was 300-800nm. Then the prepared ZSM-48 molecular sieve was ion exchanged 3 times in 0.5mol / L ammonia solution and roasted at 600℃ for 6h to obtain an active ZSM-48 molecular sieve.

[0108] (3) Preparation of Hydroisomerization Catalyst

[0109] The active ZSM-48 molecular sieve prepared above was mixed with SB powder in a weight ratio of 65%:35%, and a shaped carrier was prepared by the kneading-extrusion method. It was then immersed in a palladium chloride solution, dried at 60°C for 6 hours, and calcined at 400°C for 6 hours to obtain a hydroisomerization catalyst with a metal Pd loading of 0.50%. The test results of the obtained hydroisomerization catalyst are shown in Table 16.

[0110] (4) Preparation of lubricating oil base oil

[0111] The Fischer-Tropsch wax with a distillation range of 400-550°C is used as a raw material, and a hydroisomerization reaction is carried out under the action of the hydroisomerization catalyst prepared above, and a hydrorefining reaction is carried out under the action of a hydrorefining catalyst with Pt as an active metal and macroporous alumina as a carrier. The temperature of the hydroisomerization reaction is 340°C, the hydrogen partial pressure is 3MPa, and the volume space velocity is 1.0h -1 , the hydrogen-oil volume ratio is 800:1; the temperature of the hydrotreating reaction is 240°C, and the volume space velocity is 1.0h -1 , the hydrogen-oil volume ratio is 800:1, and the hydrogen partial pressure is 3MPa. The obtained hydrorefined product is separated under atmospheric distillation conditions to obtain naphtha with a fraction less than 160°C and a light white oil fraction with a fraction of 160-260°C, and under reduced pressure distillation conditions to obtain lubricating oil base oils, including 2cSt base oil with a fraction of 260-370°C, 3cSt base oil with a fraction of 370-400°C, 4cSt base oil with a fraction of 400-450°C, and 6cSt base oil with a fraction of more than 450°C. The test data of the obtained base oils are shown in Table 6.

[0112] Table 6

[0113]

[0114] Example 7

[0115] (1) Synthetic seed crystals

[0116] Take 1.2g of sodium hydroxide, 0.4g of sodium aluminate, 2g of template, 60g of silica sol and 60g of water, mix and stir evenly, and place in a crystallization kettle for crystallization at a temperature of 170°C for 32h. After the crystallization is completed, cool, filter, wash, dry and roast to obtain ZSM-48 seed crystals. The washing solvent is water, the drying temperature is 120°C for 4h, and the roasting temperature is 600°C for 6h.

[0117] (2) Preparation of active molecular sieves

[0118] 1.2g of sodium hydroxide, 0.45g of sodium aluminate, 2.2g of template, 65g of silica sol, 65g of water and seed crystals were mixed and stirred evenly and then placed in a crystallization kettle for staged crystallization, wherein the concentration of seed crystals in the above crystallization system is 2000ppm, the temperature of the first stage of crystallization is 110℃, the time is 8h, the temperature of the first stage of crystallization is 180℃, the time is 28h, after the crystallization is completed, the ZSM-48 molecular sieve is obtained by cooling, suction filtration, washing, drying and roasting, wherein the washing solvent is water, the drying temperature is 80℃, the time is 10h, the roasting temperature is 500℃, the time is 10h, the silicon-aluminum ratio of the molecular sieve is 180, the axial size of the molecular sieve is 2-5μm, and the radial size is 800-1000nm. Then the prepared ZSM-48 molecular sieve is ion exchanged once in 10mol / L ammonia solution and roasted at 500℃ for 10h to obtain an active ZSM-48 molecular sieve.

[0119] (3) Preparation of Hydroisomerization Catalyst

[0120] The active ZSM-48 molecular sieve prepared above was mixed with SB powder in a weight ratio of 65%:35%, and a shaped carrier was prepared by the kneading-extrusion method. It was then immersed in a tetraammine dinitrate platinum solution, dried at 120°C for 4 hours, and calcined at 600°C for 2 hours to obtain a hydroisomerization catalyst with a metal Pt loading of 0.50%. The test results of the obtained hydroisomerization catalyst are shown in Table 16.

[0121] (4) Preparation of lubricating oil base oil

[0122] The Fischer-Tropsch wax with a distillation range of 400-550°C is used as a raw material, and a hydroisomerization reaction is carried out under the action of the hydroisomerization catalyst prepared above, and a hydrorefining reaction is carried out under the action of a hydrorefining catalyst with Pt as an active metal and macroporous alumina as a carrier. The temperature of the hydroisomerization reaction is 340°C, the hydrogen partial pressure is 3MPa, and the volume space velocity is 1.0h -1 , the hydrogen-oil volume ratio is 800:1; the temperature of the hydrotreating reaction is 240°C, and the volume space velocity is 1.0h -1 , the hydrogen-oil volume ratio is 800:1, and the hydrogen partial pressure is 3MPa. The obtained hydrorefined product is separated under atmospheric distillation conditions to obtain naphtha with a fraction less than 160°C and a light white oil fraction with a fraction of 160-260°C, and under reduced pressure distillation conditions to obtain lubricating oil base oils, including 2cSt base oil with a fraction of 260-370°C, 3cSt base oil with a fraction of 370-400°C, 4cSt base oil with a fraction of 400-450°C, and 6cSt base oil with a fraction of more than 450°C. The test data of the obtained base oils are shown in Table 7.

[0123] Table 7

[0124]

[0125]

[0126] Example 8

[0127] The hydroisomerization catalyst prepared in Example 3 was used to prepare lubricating oil base oil.

[0128] Preparation of lubricating oil base oil: Using Fischer-Tropsch wax with a distillation range of 400-550°C as raw material, carrying out a hydroisomerization reaction under the action of the hydroisomerization catalyst prepared above, and carrying out a hydrorefining reaction under the action of a hydrorefining catalyst with Pt as an active metal and macroporous alumina as a carrier. The temperature of the hydroisomerization reaction is 300°C, the hydrogen partial pressure is 2MPa, and the volume space velocity is 0.3h -1 , the hydrogen-oil volume ratio is 200:1; the temperature of the hydrotreating reaction is 200°C, and the volume space velocity is 0.2h -1 , the hydrogen-oil volume ratio is 2000:1, and the hydrogen partial pressure is 2MPa. The obtained hydrorefined product is separated under atmospheric distillation conditions to obtain naphtha with a fraction less than 160°C and a light white oil fraction with a fraction of 160-260°C, and under reduced pressure distillation conditions to obtain lubricating oil base oils, including 2cSt base oil with a fraction of 260-370°C, 3cSt base oil with a fraction of 370-400°C, 4cSt base oil with a fraction of 400-450°C, and 6cSt base oil with a fraction of more than 450°C. The test data of the obtained base oils are shown in Table 8.

[0129] Table 8

[0130]

[0131] Example 9

[0132] The hydroisomerization catalyst prepared in Example 3 was used to prepare lubricating oil base oil.

[0133] Preparation of lubricating oil base oil: Using Fischer-Tropsch wax with a distillation range of 400-550°C as raw material, carrying out a hydroisomerization reaction under the action of the hydroisomerization catalyst prepared above, and carrying out a hydrorefining reaction under the action of a hydrorefining catalyst with Pt as an active metal and macroporous alumina as a carrier. The temperature of the hydroisomerization reaction is 380°C, the hydrogen partial pressure is 10MPa, and the volume space velocity is 2h -1 , the hydrogen-oil volume ratio is 2000:1; the temperature of the hydrotreating reaction is 280℃, and the volume space velocity is 2h -1, the hydrogen-oil volume ratio is 200:1, and the hydrogen partial pressure is 10MPa. The obtained hydrorefined product is separated under atmospheric distillation conditions to obtain naphtha with a fraction less than 160°C and a light white oil fraction with a fraction of 160-260°C, and under reduced pressure distillation conditions to obtain lubricating oil base oils, including 2cSt base oil with a fraction of 260-370°C, 3cSt base oil with a fraction of 370-400°C, 4cSt base oil with a fraction of 400-450°C, and 6cSt base oil with a fraction of more than 450°C. The test data of the obtained base oils are shown in Table 9.

[0134] Table 9

[0135]

[0136] Example 10

[0137] The hydroisomerization catalyst prepared in Example 3 was used to prepare lubricating oil base oil.

[0138] Preparation of lubricating oil base oil: Using Fischer-Tropsch wax with a distillation range of 400-550°C as raw material, carrying out a hydroisomerization reaction under the action of the hydroisomerization catalyst prepared above, and carrying out a hydrorefining reaction under the action of a hydrorefining catalyst with Pt as an active metal and macroporous alumina as a carrier. The temperature of the hydroisomerization reaction is 310°C, the hydrogen partial pressure is 8MPa, and the volume space velocity is 0.5h -1 The hydrogen-oil volume ratio is 1500:1; the temperature of the hydrotreating reaction is 260°C, and the volume space velocity is 1.6h -1 , the hydrogen-oil volume ratio is 500:1, and the hydrogen partial pressure is 8MPa. The obtained hydrorefined product is separated under atmospheric distillation conditions to obtain naphtha with a fraction less than 160°C and a light white oil fraction with a fraction of 160-260°C, and under reduced pressure distillation conditions to obtain lubricating oil base oils, including 2cSt base oil with a fraction of 260-370°C, 3cSt base oil with a fraction of 370-400°C, 4cSt base oil with a fraction of 400-450°C, and 6cSt base oil with a fraction of more than 450°C. The test data of the obtained base oils are shown in Table 10.

[0139] Table 10

[0140]

[0141]

[0142] Embodiment 11

[0143] The hydroisomerization catalyst prepared in Example 3 was used to prepare lubricating oil base oil.

[0144] Preparation of lubricating oil base oil: Using Fischer-Tropsch wax with a distillation range of 400-550°C as raw material, carrying out a hydroisomerization reaction under the action of the hydroisomerization catalyst prepared above, and carrying out a hydrorefining reaction under the action of a hydrorefining catalyst with Pt as an active metal and macroporous alumina as a carrier. The temperature of the hydroisomerization reaction is 360°C, the hydrogen partial pressure is 3MPa, and the volume space velocity is 1.5h -1 , the hydrogen-oil volume ratio is 500:1; the temperature of the hydrotreating reaction is 220℃, and the volume space velocity is 0.5h -1 , the hydrogen-oil volume ratio is 1500:1, and the hydrogen partial pressure is 3MPa. The obtained hydrorefined product is separated under atmospheric distillation conditions to obtain naphtha with a fraction less than 160°C and a light white oil fraction with a fraction of 160-260°C, and under reduced pressure distillation conditions to obtain lubricating oil base oils, including 2cSt base oil with a fraction of 260-370°C, 3cSt base oil with a fraction of 370-400°C, 4cSt base oil with a fraction of 400-450°C, and 6cSt base oil with a fraction of more than 450°C. The test data of the obtained base oils are shown in Table 11.

[0145] Table 11

[0146]

[0147]

[0148] Example 12

[0149] (1) Synthetic seed crystals

[0150] The seed crystals prepared in Example 1 were used as seed crystals for preparing ZSM-48 molecular sieve in this example.

[0151] (2) Preparation of active molecular sieves

[0152] 1.4 g of sodium hydroxide, 0.55 g of sodium aluminate, 2.1 g of template, 60 g of silica sol, 65 g of water and seed crystals were mixed and stirred evenly, and then placed in a crystallization kettle for staged crystallization, wherein the concentration of seed crystals in the above crystallization system is 6000 ppm, the temperature of the first stage of crystallization is 100°C, the time is 12 h, the temperature of the second stage of crystallization is 170°C, and the time is 24 h. After the crystallization is completed, the ZSM-48 molecular sieve is obtained by cooling, filtering, washing, drying and calcining, wherein the washing solvent is water, the drying temperature is 120°C, the time is 6 h, the calcination temperature is 500°C, the time is 6 h, the silicon-aluminum ratio of the molecular sieve is 110, the axial size of the molecular sieve is 2.0-2.5 μm, and the radial size is 550-700 nm. Then, the prepared ZSM-48 molecular sieve was ion exchanged three times in 1 mol / L ammonium nitrate solution and calcined at 500° C. for 10 h to obtain an active ZSM-48 molecular sieve.

[0153] (3) Preparation of Hydroisomerization Catalyst

[0154] The active ZSM-48 molecular sieve prepared above was mixed with SB powder in a weight ratio of 70%:30%, and a shaped carrier was prepared by the kneading-extrusion method. It was then immersed in a 1 mol / L ammonia solution and dried and calcined at 100°C for 5 h to obtain a hydroisomerization catalyst with a metal Pt loading of 0.45%. The test results of the obtained hydroisomerization catalyst are shown in Table 16.

[0155] (4) Preparation of lubricating oil base oil

[0156] The Fischer-Tropsch wax with a distillation range of 400-550°C is used as a raw material, and a hydroisomerization reaction is carried out under the action of the hydroisomerization catalyst prepared above, and a hydrorefining reaction is carried out under the action of a hydrorefining catalyst with Pt / Pd as an active metal and macroporous alumina as a carrier. The temperature of the hydroisomerization reaction is 335°C, the hydrogen partial pressure is 3.5MPa, and the volume space velocity is 0.8h -1 , the hydrogen-oil volume ratio is 600:1; the temperature of the hydrotreating reaction is 240°C, and the volume space velocity is 1h -1 , the hydrogen-oil volume ratio is 800:1, and the hydrogen partial pressure is 3.5MPa. The obtained hydrorefined product is separated under atmospheric distillation conditions to obtain naphtha with a fraction less than 160°C and a light white oil fraction with a fraction of 160-260°C, and under reduced pressure distillation conditions to obtain lubricating oil base oils, including 2cSt base oil with a fraction of 260-370°C, 3cSt base oil with a fraction of 370-400°C, 4cSt base oil with a fraction of 400-450°C, and 6cSt base oil with a fraction of more than 450°C. The test data of the obtained base oils are shown in Table 12.

[0157] Table 12

[0158]

[0159]

[0160] Comparative Example 1

[0161] (1) Preparation of active molecular sieves

[0162] 0.9g of sodium hydroxide, 0.85g of sodium aluminate, 2.1g of template agent, 60g of silica sol and 65g of water were mixed and stirred evenly and then placed in a crystallization kettle for crystallization. The crystallization temperature was 170°C and the time was 28h. After the crystallization was completed, the ZSM-48 molecular sieve was obtained by cooling, filtration, washing, drying and calcination. The washing solvent was water, the drying temperature was 120°C and the time was 4h. The calcination temperature was 500°C and the time was 6h. The silicon-aluminum ratio of the molecular sieve was 70, and the axial size of the molecular sieve was 2.5-3.0μm and the radial size was 600-800nm. Then the prepared ZSM-48 molecular sieve was ion exchanged 3 times in 1mol / L ammonium nitrate solution and calcined at 500°C for 6h to obtain an active ZSM-48 molecular sieve.

[0163] (2) Preparation of Hydroisomerization Catalyst

[0164] The active ZSM-48 molecular sieve prepared above was mixed with SB powder in a weight ratio of 65%:35%, and a shaped carrier was prepared by the kneading-extrusion method. It was then immersed in a 1 mol / L ammonia solution, dried at 100°C for 4 h, and calcined at 400°C for 6 h to obtain a hydroisomerization catalyst with a metal Pt loading of 0.40%. The test results of the obtained hydroisomerization catalyst are shown in Table 16.

[0165] (3) Preparation of lubricating oil base oil

[0166] The Fischer-Tropsch wax with a distillation range of 400-550°C is used as a raw material, and a hydroisomerization reaction is carried out under the action of the hydroisomerization catalyst prepared above, and a hydrorefining reaction is carried out under the action of a hydrorefining catalyst with Pt / Pd as an active metal and macroporous alumina as a carrier. The temperature of the hydroisomerization reaction is 337°C, the hydrogen partial pressure is 3.5MPa, and the volume space velocity is 0.7h -1 , the hydrogen-oil volume ratio is 800:1; the temperature of the hydrotreating reaction is 240°C, and the volume space velocity is 1h -1 , the hydrogen-oil volume ratio is 800:1, and the hydrogen partial pressure is 3.5MPa. The obtained hydrorefined product is separated under atmospheric distillation conditions to obtain lubricating oil base oil. The test data of the obtained base oil is shown in Table 13.

[0167] Table 13

[0168]

[0169]

[0170] Comparative Example 2

[0171] (1) Preparation of active molecular sieves

[0172] 1.2g of sodium hydroxide, 0.3g of sodium aluminate, 2g of template agent, 60g of silica sol and 60g of water were mixed and stirred evenly and then placed in a crystallization kettle for crystallization. The crystallization temperature was 180°C and the time was 24h. After the crystallization was completed, the ZSM-48 molecular sieve was obtained by cooling, filtration, washing, drying and roasting. Among them, the washing solvent was water, the drying temperature was 100°C, the time was 5h, the roasting temperature was 500°C, the time was 8h, the silicon-aluminum ratio of the molecular sieve was 190, the axial size of the molecular sieve was 1.5-2.0μm, and the radial size was 500-650nm. Then the prepared ZSM-48 molecular sieve was ion exchanged 3 times in 1mol / L ammonium nitrate solution and roasted at 600°C for 6h to obtain an active ZSM-48 molecular sieve.

[0173] (2) Preparation of Hydroisomerization Catalyst

[0174] The active ZSM-48 molecular sieve prepared above was mixed with SB powder in a weight ratio of 75%:25%, and a shaped carrier was prepared by a kneading-extrusion method. The carrier was then immersed in a tetraammineplatinum dichloride solution, dried at 60°C for 4 hours, and calcined at 400°C for 6 hours to obtain a hydroisomerization catalyst with a metal Pt loading of 0.35%. The test results of the obtained hydroisomerization catalyst are shown in Table 16.

[0175] (4) Preparation of lubricating oil base oil

[0176] The Fischer-Tropsch wax with a distillation range of 400-550°C is used as a raw material, and a hydroisomerization reaction is carried out under the action of the hydroisomerization catalyst prepared above, and a hydrorefining reaction is carried out under the action of a hydrorefining catalyst with Pt as an active metal and macroporous alumina as a carrier. The temperature of the hydroisomerization reaction is 350°C, the hydrogen partial pressure is 3.5MPa, and the volume space velocity is 0.8h -1 , the hydrogen-oil volume ratio is 800:1; the temperature of the hydrotreating reaction is 240°C, and the volume space velocity is 1h -1 , the hydrogen-oil volume ratio is 800:1, and the hydrogen partial pressure is 3.5MPa. The obtained hydrorefined product is separated under atmospheric distillation conditions to obtain lubricating oil base oil. The test data of the obtained base oil is shown in Table 14.

[0177] Table 14

[0178]

[0179]

[0180] The distillation range data of the Fischer-Tropsch wax raw material with a distillation range of 400-550° C. used in the examples and comparative examples were tested, and the results are shown in Table 15.

[0181] Table 15

[0182] Rec mass(%) BP, (℃) IBP 396.0 5 405.5 10 408.5 20 427.5 30 436.5 40 445.0 50 452.5 60 460.5 70 470.5 80 482.5 90 506.5 95 545.0 FBP 700.0

[0183] The hydroisomerization catalysts prepared in Examples 1 to 12 and Comparative Examples 1 to 2 were tested for relevant performances, and the yield of the prepared base oil and the yields of 2cSt base oil, 3cSt base oil, 4cSt base oil, and 6cSt base oil in the base oil were recorded. The results are shown in Table 16.

[0184] Table 16

[0185]

[0186] From the above description, it can be seen that the above embodiments of the present invention achieve the following technical effects: Embodiments 1 to 7 are the preparation of lubricating base oil using the hydroisomerization catalyst prepared by the preparation method of the present invention. Since the prepared catalyst has a suitable specific surface area, weak acid content and medium-strong acid content, it has a good matching effect on the Fischer-Tropsch wax with a distillation range of 400 to 550°C described in the present invention. Therefore, the lubricating base oil prepared not only has a high yield, but also has the advantages of high viscosity index, low pour point and low cloud point. At the same time, the preparation method can also simultaneously produce 4cSt base oil and 6cSt base oil with higher quality.

[0187] Examples 8 to 11 further optimize the conditions of the hydroisomerization reaction and the conditions of the hydrofining reaction. The conditions for controlling the hydroisomerization reaction and the hydrofining reaction have good effects within the scope of the present invention. It is worth mentioning that under the action of the hydroisomerization catalyst of the present invention, even if the pressure of the hydroisomerization reaction and the hydrofining reaction is controlled under lower conditions, good reaction results can be achieved, and there is no need to increase the reaction pressure to achieve the purpose of improving the reaction yield. In the process of large-scale production, the purpose of reducing energy consumption can be further achieved. In the process of preparing the hydroisomerization catalyst, Example 12 increases the amount of seed added in the crystallization reaction system. This measure does not effectively help to improve the catalytic effect of the catalyst, and the quality of the lubricating oil base oil prepared is slightly worse than that of the lubricating oil base oil prepared in the embodiment of the present invention. In addition, the increase in the amount of seed added also wastes the seed, resulting in waste, especially in the process of large-scale production, which will increase the production cost.

[0188] In the process of preparing the hydroisomerization catalyst in Comparative Example 1, no seed crystals were added; in the process of preparing the hydroisomerization catalyst in Comparative Example 2, not only no seed crystals were added, but the silicon-aluminum ratio of the catalyst molecular sieve carrier was also not outside the protection scope of the present invention. The catalytic effect of the obtained hydroisomerization catalyst was significantly different from that of the catalyst of the present invention. The quality of the lubricating base oil prepared was also worse. At the same time, the quality of the 4cSt base oil and 6cSt base oil produced was also relatively poor.

[0189] In summary, by using the hydroisomerization catalyst prepared by the preparation method of the present invention to prepare lubricating base oil, and controlling the specific surface area, weak acid content and medium-strong acid content of the prepared catalyst within an appropriate range, the hydroisomerization catalyst can be matched well with the Fischer-Tropsch wax with a distillation range of 400 to 550° C. The prepared lubricating base oil not only has a high yield, but also has the advantages of high viscosity index, low pour point and low cloud point. At the same time, the lubricating base oil preparation method can also simultaneously produce 4cSt base oil and 6cSt base oil with higher quality.

[0190] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims

1. A method for preparing a lubricating oil base oil, characterized in that: The preparation method comprises: subjecting Fischer-Tropsch wax having a distillation range of 400 to 550° C. to a hydroisomerization reaction under the action of a hydroisomerization catalyst, and then subjecting the lubricating oil base oil to a hydrorefining reaction and distillation under the action of a hydrorefining catalyst; wherein the preparation method of the hydroisomerization catalyst comprises the following steps: Step (1), mixing an alkali, an aluminum source, a template, a silicon source and water to form a mixed solution, and subjecting the mixed solution to a crystallization reaction to obtain a reaction solution A; Step (2), cooling, filtering, washing, first drying and first calcining the reaction solution A to obtain ZSM-48 seed crystals; Step (3), preparing ZSM-48 molecular sieve according to the preparation method of step (1) and step (2), and adding the ZSM-48 seed crystals when preparing the mixed solution; Step (4), subjecting the ZSM-48 molecular sieve to ammonium exchange and a second calcination to obtain an active ZSM-48 molecular sieve; Step (5), mixing the active ZSM-48 molecular sieve with a binder and molding to obtain a molded carrier; Step (6), loading the shaped carrier with noble metal ions, and then subjecting the shaped carrier to a second drying and a third calcination to obtain the hydroisomerization catalyst.

2. The method for preparing a lubricating oil base oil according to claim 1, characterized in that: The saturated hydrocarbon content of the Fischer-Tropsch wax is ≥ 90%; Preferably, the concentration of the seed crystals in the crystallization reaction system formed in step (3) is 2000 to 5000 ppm.

3. The method for preparing a lubricating oil base oil according to claim 1, characterized in that: The ammonium exchange process comprises: treating the ZSM-48 molecular sieve with ammonia water or a salt containing ammonium ions; Preferably, the salt containing ammonium ions is ammonium nitrate.

4. The method for preparing a lubricating base oil according to any one of claims 1 to 3, characterized in that: The crystallization is one-stage crystallization or segmented crystallization; Preferably, the temperature of the first stage of crystallization is 160-180°C; Preferably, the staged crystallization temperature is 100-180°C; Preferably, the crystallization time is 20 to 48 hours; Preferably, the staged crystallization is two stage crystallizations performed sequentially, the first stage crystallization temperature of the two stage crystallizations is less than the second stage crystallization temperature, and the difference between the first stage crystallization temperature and the second stage crystallization temperature is 40-80° C.; Preferably, in the staged crystallization, the first stage crystallization time is 8 to 20 hours, and the second stage crystallization time is 12 to 33 hours.

5. The method for preparing a lubricating base oil according to any one of claims 1 to 3, characterized in that: The silicon-aluminum ratio of the ZSM-48 molecular sieve is 70 to 180; Preferably, the specific surface area of ​​the ZSM-48 molecular sieve is 200 to 250 m 2 / g Preferably, the weight ratio of the ZSM-48 molecular sieve and the binder in the shaped carrier is (65-75) %: (25～35)％； Preferably, the binder is SB powder; Preferably, the ZSM-48 molecular sieve is a rod-shaped structure; Preferably, the ZSM-48 molecular sieve has an axial size of 0.5 to 5 μm and a radial size of 300 to 1000 nm.

6. The method for preparing a lubricating base oil according to any one of claims 1 to 3, characterized in that: The process of loading the shaped carrier with the noble metal ions in step (5) is: immersing the shaped carrier in a solution containing the noble metal ions once or in several times; Preferably, the loading amount of the noble metal ions is 0.3-0.5%; Preferably, when loading in stages, the first loading amount is 0.1-0.3%, and the second loading amount is 0.1-0.2%; Preferably, the noble metal is Pt and / or Pd; Preferably, the Pt source is one or more of chloroplatinic acid, tetraammineplatinum dichloride and tetraammineplatinum dinitrate; Preferably, the Pd source is palladium chloride.

7. The method for preparing a lubricating base oil according to any one of claims 1 to 3, characterized in that: The hydroisomerization catalyst has a weak acid content of 0.20 to 0.35 mmol / g and a medium-strong acid content of 0.10 to 0.25 mmol / g; Preferably, the specific surface area of ​​the hydroisomerization catalyst is 200 to 250 m 2 ·g -1 .

8. The method for preparing a lubricating base oil according to any one of claims 1 to 7, characterized in that: The temperature of the hydroisomerization reaction is 300-380°C, the hydrogen partial pressure is 2-10 MPa, and the volume space velocity is 0.3-2 h -1 , the volume ratio of hydrogen to oil is (200-2000):1; Preferably, the temperature of the hydroisomerization reaction is 310-360°C, the hydrogen partial pressure is 3-8 MPa, and the volume space velocity is 0.5-1.5 h -1 , the volume ratio of hydrogen to oil is (500~1500):

1.

9. The method for preparing a lubricating base oil according to any one of claims 1 to 7, characterized in that: The temperature of the hydrofining reaction is 200-280°C, and the volume space velocity is 0.2-2h -1 , hydrogen-oil volume ratio is (200-2000):1, hydrogen partial pressure is 2-10MPa; Preferably, the temperature of the hydrofining reaction is 220-260°C, and the volume space velocity is 0.5-1.6h -1 , the volume ratio of hydrogen to oil is (500-1500):1, and the hydrogen partial pressure is 3-8MPa; Preferably, the hydrotreating catalyst comprises an active metal and a carrier for supporting the active metal, wherein the active metal is one or more of Pt, Pd, Ni and W, and the carrier is at least one of macroporous alumina and silicon aluminum oxide; Preferably, the active metal is Pt and / or Pd; Preferably, the carrier is macroporous alumina; Preferably, the loading amount of the active metal in the hydrotreating catalyst is 0.3-0.5%.

10. A lubricating oil base oil, characterized in that: The lubricating oil base oil prepared by the preparation method according to any one of claims 1 to 9 includes a 2cSt base oil with a fraction of 260-370°C, a 3cSt base oil with a fraction of 370-400°C, a 4cSt base oil with a fraction of 400-450°C and a 6cSt base oil with a fraction above 450°C.

Images