JP2006502295A - Lubricating oil hydroisomerization system - Google Patents

Abstract

The present invention relates to a one-dimensional intermediate pore molecular sieve having a substantially circular pore structure with an average diameter of 0.50 to 0.65 nm and a difference between a maximum diameter and a minimum diameter of ≦ 0.05 nm, then molecular The present invention relates to a method for converting a wax having a heavy component into a high-quality lubricating base oil using a sieve zeolite beta catalyst. Both catalysts comprise one or more Group VIII metals. For example, a cascaded two-bed catalyst system consisting of a first bed Pt / ZSM-48 catalyst followed by a second bed Pt / zeolite beta catalyst improves the processing of heavy lubricants.

Description

  The present invention relates to a method for converting a waxy raw material into a lubricating base oil having a low viscosity.

  There is an inherent economic motive to convert waxes to high quality lubricating base oils, in particular to base oils with properties and performances equivalent to or superior to those of polyalphaolefins (PAO). . Wax quality improvement relies heavily on advances in wax isomerization technology that selectively transforms linear paraffins into hyperbranched isoparaffins.

  Methods for converting wax to paraffinic lubricating base oil are known. A typical process is a two-stage process in which the wax is hydroisomerized into a waxy isoparaffin mixture in the first step, followed by solvent dewaxing or catalytic dewaxing of the waxy isoparaffin mixture in the second step to form a residual wax. To achieve the target lubricant pour point.

  Previously disclosed hydroisomerization catalysts, such as amorphous aluminosilicates and Pt supported on zeolite beta (beta), are usually large, allowing the formation of branched structures during paraffin isomerization Has pores. Examples of other large pore molecular sieves include ZSM-3, ZSM-12, ZSM-20, MCM-37, MCM-68, ECR-5, SAPO-5, SAPO-37 and USY. However, these large pore catalysts are not selective enough to preferentially convert normal and slightly branched paraffin waxes in the presence of hyperbranched isoparaffin molecules. As a result, isoparaffin products derived from wax often contain residual wax and need to be dewaxed to meet the target lube cloud point or pour point. The cloud point of the lubricating oil is the temperature at which the initial traces of wax begin to separate, causing the lubricating oil to become cloudy or cloudy (eg, ASTM D2500). The pour point of the lubricating oil is the temperature at which the lubricating oil and wax crystallize together as a whole and do not flow when poured (eg, ASTM D97). Dewaxing can be accomplished by additionally using either a solvent dewaxing method or a catalytic dewaxing method.

  The most selective dewaxing catalyst used in the catalytic dewaxing process has a relatively small pore structure and reduces the pour point of the lubricating oil by selectively cracking normal and slightly branched paraffin waxes. Catalytic effect. Such dewaxing catalysts usually have low paraffin isomerization selectivity.

  Only a few catalysts have been reported that efficiently catalyze both hydroisomerization and dewaxing of paraffin waxes, resulting in a low pour point lubricating oil. Such catalysts are also difficult to convert feedstocks with high molecular weight components, and as a result, lubricating oil products often have a haze (or cloudy) appearance.

US Pat. No. 5,075,269 US Pat. No. 3,354,078 US Pat. No. 6,090,989 Journal of Catalysis, Volume 4, 527 (1965) Journal of Catalysis, Vol. 6, page 278 (1966) Journal of Catalysis, Vol. 61, page 395 (1980)

  Accordingly, there remains a need to achieve high molecular weight wax conversion and sufficiently low pour point without sacrificing isomerization dewaxing selectivity of the lubricating oil.

  The present invention relates waxes to one-dimensional molecular sieve catalysts (eg ZSM) having a substantially circular pore structure with an average diameter of 0.50 to 0.65 nm and a difference between the maximum and minimum diameters ≦ 0.05 nm. -48) and then to a process for converting wax to a high quality lubricating base oil by contacting with a second molecular sieve catalyst (eg zeolite beta). Both catalysts comprise one or more Group VIII metals (ie Fe, Ru, Os, Co, Rh, Ir, Pd, Pt, Ni).

  The present invention has an average diameter of 0.50 to 0.65 nm (5.0 to 6.5 angstroms) and a maximum diameter minus a minimum diameter ≦ 0.05 nm (0.5 angstrom) for producing a lubricating oil. It provides a high degree of wax isomerization and dewaxing selectivity over a one-dimensional catalyst having a substantially circular pore structure and then on a molecular sieve catalyst. On these two catalysts, Group VIII metals are preferred, with platinum being most preferred.

  The present invention improves lubricating base oil products and their properties (eg, pour point, cloud point). The method effectively reduces the average lube molecular weight and potentially reduces the cloud point of the lube oil product without sacrificing lube oil yield. This method makes it possible to improve the use of heavy fractions of lubricating oils and is particularly suitable for waxes having 1,000 ° F. + fractions, preferably 1,100 ° F. + fractions. These fractions may contain high molecular weight or high boiling tails of the raw material. If only one of the above catalysts is used, it may be difficult to create sufficient branching with minimal cracking for very high molecular weight feeds. The present invention is preferably used to treat heavy lubricating oils or lubricating oils having heavy components (e.g., having> 5 wt% heavy raffinate), in which case the beta catalyst is Selectively break up minutes. According to the present invention, a light lubricating oil can be obtained in a yield similar to that obtained on ZSM-48 alone.

  The wax feed is preferably first passed over the ZSM-48 catalyst. The resulting intermediate product is then passed over a single zeolite beta catalyst to produce the final lubricating oil. These first and second stages can be separated or are preferably integrated process steps (eg, cascaded).

  A one-dimensional molecular sieve catalyst having a substantially circular pore structure provides most dewaxing. The pores are smaller than in the case of large pore molecular sieves, thereby eliminating bulky (eg, highly branched) molecules. One dimension means that the pores are substantially parallel to each other.

  The pores of the catalyst have an average diameter of 0.50 nm to 0.65 nm, where the difference between the minimum and maximum diameter is ≦ 0.05 nm. The pores do not necessarily have a perfect circular or elliptical cross section. The minimum and maximum diameters are just the dimensions of an ellipse with a cross-sectional area approximately equal to the cross-sectional area of the average pore. Alternatively, the pores can be defined by finding the center of the pore cross-section and sweeping the pore shape of the average cross-sectional area from this center using half the smallest diameter and half the largest diameter.

  A preferred one-dimensional molecular sieve catalyst is a medium pore molecular sieve catalyst, of which the preferred type is ZSM-48. Patent Document 1 describes a procedure for producing ZSM-48, which is incorporated herein by reference. ZSM-48 is approximately 65% zeolite crystals and 35% alumina. Of the crystals, at least 90%, preferably at least 95%, most preferably 98-99% are complete crystals. ZSM-48 can tolerate some sodium, but the protonated form is preferred. ZSM-48 is robust compared to other catalysts with similar functions and helps protect a second catalyst (eg, zeolite beta).

  In the first stage of the process, a one-dimensional mesoporous molecular sieve catalyst (eg, Pt / ZSM-48) is heated to 500-800 ° F. (260-427 ° C.), more preferably 600-700 ° F. 316-371 ° C.), most preferably 630-660 ° F. (332-349 ° C.). The ZSM-48 catalyst used in the present invention preferably has an alpha value of about 10 to about 50 prior to Group VIII metal loading.

  The zeolite beta catalyst is a 12-membered acidic silica / alumina zeolite with or without boron (which replaces some of the aluminum atoms). Zeolite Y (USY) is also contemplated within the scope of the present invention, although less preferred than beta. If some residual sulfur is acceptable in the product, presulfided zeolite beta is preferred.

  The zeolite beta used in the present invention preferably has an alpha value of less than 15, more preferably less than 10, at least prior to metal filling. The alpha value is an acidity metric and is an approximate indication of the catalytic cracking activity of the catalyst compared to the standard catalyst. The alpha value is a relative rate constant (rate of normal hexane conversion per catalyst volume per unit time). The alpha value is based on the activity of the highly active silica-alumina cracking catalyst, which is taken as alpha 1 in US Pat. As described in Non-Patent Document 3, measurement is performed at 538 ° C. A feed with the lowest nitrogen content will require a low alpha value for this catalyst. In contrast, catalysts with high alpha values are used when the selective cracking is small. The alpha value can be reduced by steam treatment.

  The beta catalyst (eg, Pt / beta), when in contact with the intermediate product, is 400-700 ° F. (204-371 ° C.), more preferably 500-650 ° F. (260-343 ° C.), most preferably 520 Most preferably, the temperature is maintained at ˜580 ° F. (271-304 ° C.).

The temperature of each catalyst is preferably controlled independently. The selection of temperature depends partly on the liquid hourly space velocity, of which 0.1 to 20 h ⁻¹ is preferable, 0.5 to 5 h ⁻¹ is more preferable, and 0.5 to 2 h ⁻¹ is most preferable.

The contact times of both catalysts are preferably approximately the same. It will be appreciated that the space velocity may be different. The pressures of both catalysts are preferably approximately the same. The hydrogen co-feeding flow rate is 100 to 10,000 scf / bbl (17.8 to 1,780 nL.L ⁻¹ ), more preferably 1,000 to 6,000 scf / bbl (178 to 1,068 nL.L.1). the L ^-1) and most preferably 1,500~3,000scf / bbl (267~534n.L.L ^-1).

  Each catalyst comprises 0.01 to 5% by weight of at least one Group VIII metal (i.e. Fe, Ru, Os, Co, Rh, Ir, Pd, Pt, Ni). Platinum and palladium are most preferred. The selection of platinum or palladium blended with each other or with other Group VIII metals follows. Nickel can also be blended with Group VIII noble metals and is included within the scope of the present invention whenever reference is made to a blend, alloy or mixture with Group VIII. Platinum is the most preferred metal. A suitable metal loading on both catalysts is 0.1 to 1 wt%, with about 0.6 wt% being most preferred.

  The feedstock is preferably a wax having a melting point above 50 ° C., less than 7,000 ppm sulfur, and less than 50 ppm nitrogen. More preferably, the nitrogen is less than 10 ppm nitrogen when the hydrogen pressure is less than 500 psig (34 atm). For example, heavy raffinate can be blended with a Fischer-Tropsch wax or similar clean waxy feed (eg, to reduce sulfur and / or nitrogen levels).

  The feed is preferably converted by the first catalyst to produce an intermediate product which is then passed directly from the first catalyst to the second catalyst. In a preferred embodiment of the invention, a cascaded two-bed catalyst system consisting of a first bed catalyst followed by a second bed catalyst for wax isomerization and lube hydrodewaxing with minimal gas production. Enables highly selective processes. In cascading, it is preferred to pass the intermediate product directly from the first bed to the second bed without interstage removal of light products. Optionally, light by-products (eg, methane, ethane) can be removed between the first and second catalysts.

  High branching in the feed helps the present invention and improves the final lubricant yield. U.S. Patent No. 6,057,031 describes a representative branching index, which is incorporated by reference. The feed is preferably mixed with hydrogen and preheated before contacting it with the first catalyst. Preferably, at least 95% of the wax is in a liquid state prior to contacting it with the first catalyst.

As taught by the standard, suitable measurement methods are described in this paragraph. If there are two values, the value in parentheses is the approximate metric equivalent of the first value. The weight percent of paraffin can be measured by high resolution ¹ H-NMR, for example, by the method described in ASTM standard D5292 in combination with GC-MS. This approach can also be used to determine the weight percentage of unsaturated compounds, alcohols, oxygenates, and other organic components. The ratio of iso to normal paraffin can be measured by performing gas chromatography (GC) or GC-MS in combination with ¹³ C-NMR. Sulfur can be measured by XRF (fluorescent X-ray), for example, as described in ASTM standard D2622. Nitrogen can be measured by syringe / inlet oxidative combustion and chemiluminescence detection, for example, by the method described in ASTM standard D4629. The aromatic compound can be measured as follows. As taught by the standards, olefins can be measured by using the bromine index determined by coulometric analysis, for example, by using ASTM standard D2710. The weight percent of total oxygen can be measured by neutron activation in combination with high resolution ¹ H-NMR. If necessary, the total oxygen content can be set to a water free standard by measuring the water content. For samples with a moisture content known to be less than about 200 ppm by weight, a known derivatization method (eg, by using calcium carbide to produce acetylene) followed by GC-MS Can be used. For samples with a water content known to exceed about 200 ppm by weight, the Karl-Fischer method can be used, for example, by the method described in ASTM standard D4928. The total alcohol content can be determined by high resolution ¹ H-NMR, and the percentage present primarily as C ₁₂ -C ₂₄ primary alcohol can be determined by GC-MS. The cetane number can be determined, for example, by using ASTM standard D613. The level of aromatics can be determined by using high resolution ¹ H-NMR, for example by using ASTM standard D5292. Diatomic oxygenates are measured by using infrared (IR) absorbance spectroscopy. The branching properties of iso-paraffin can be measured by a combination of high resolution ¹³ C-NMR and GC with high resolution MS.

  A cascaded two-bed catalyst system consisting of a first stage Pt / ZSM-48 catalyst, followed immediately by a second stage Pt / beta catalyst, is highly advanced for hydroisomerization and dewaxing of waxes with high molecular weight components. It was shown to be active and selective.

The operating conditions, material balance data, lubricant yield, and properties of the examples are summarized in Table 1. TBP x% indicates the temperature at which x weight percent of the hydrocarbon sample boils below that temperature. Oil passage time (TOS) is the time during which the raw material is in contact with the catalyst. IBP is the first stop point. TBP is the final boiling point. Best S.E. equivalent to standard cubic feet of hydrogen per barrel of raw material. I. (SCF / barrel) is a standard liters of hydrogen gas per Material 1 liter (n.1.l ^-1 or N.L.L ^-1, or N.L, (gas) / L (feed)) . LHSV is defined as the liquid hourly space velocity. WHSV is defined as the weight hourly space velocity.

  To obtain the desired wax isomerization results, mild (eg, 500-630 ° F. (260-332 ° C.)) Pt / beta temperatures should be used during lube oil hydroprocessing. In order to achieve the target lube pour point, a mild Pt / beta temperature should be used while varying the Pt / ZSM-48 temperature. In order to achieve the highest lubricant yield, low operating pressures (<2,000 psi (272 atm) hydrogen pressure) should be used.

  Pt / ZSM-48 alone was also evaluated for isomerization and dewaxing of C80 wax to 700 ° F + (371 ° C +) lubricating base oil (Table 2). A comparison of lubricating oil yields for the two catalyst systems is shown in FIG. FIG. 1 shows that Pt / ZSM-48 in the cascade, followed by Pt / beta, gave substantially the same lubricant yield compared to Pt / ZSM-48 alone. The addition of Pt / beta had minimal impact on the operating temperature range of Pt / ZSM-48 (Tables 1 and 2).

  The viscosity and viscosity index of the nominal 700 ° F + (371 ° C +) C80 wax isomer vs. hydroprocessing severity are plotted in FIGS. 2 and 3, respectively. The two sets of data compared in the two figures correspond to wax isomers prepared using Pt / ZSM-48, followed by Pt / beta, and Pt / ZSM-48 alone.

  As shown in FIG. 2, the Pt / ZSM-48-Pt / beta isomer was significantly less viscous, probably due to the relatively high cracking activity of the Pt / beta catalyst on multi-branched isoparaffins. Thus, this dual catalyst system is effective in producing lower viscosity lubricant base stocks by reducing the average molecular weight of the wax feed without sacrificing the lubricant yield during the wax hydroisomerization process. Provide a simple way.

  FIG. 3 shows that the high viscosity index observed for the Pt / ZSM-48-Pt / beta wax isomer is slightly lower than that of the Pt / ZSM-48 isomer. The product of the present invention preferably has a viscosity index of at least 150 at a lubricating oil pour point of −20 ° C. and a viscosity index of at least 130 at a pour point of −50 ° C. or lower.

  In the case of Pt / ZSM-48-Pt / Beta, the spread between the cloud point and pour point of the lubricant is mostly below 15 ° C. (Table 1). In general, the spread between the cloud point and pour point of the lubricating oil becomes narrower as the pour point decreases.

  For the two catalyst systems, the overall light by-product selectivity is comparable (FIGS. 4-6). As expected, the yields of gas, naphtha, and diesel oil increase in both systems with increasing process severity (reducing lube pour point) that facilitates hydrocracking.

  The following examples will serve to illustrate the present invention.

Example 1
Feedstock Oil-treated SASOL® PARAFLINT® C80 wax (C80) feedstock was prepared from Moore and Munger, Inc. (Shelton, Conn.) Shelton)) and used as received without additional pretreatment. The C80 wax was a mixture of mainly linear paraffins and very low contents of olefins and oxygenates. Sazol® is marketed in three commercial grades of wax: 700 ° F + (371 ° C +) wax with all types of Paraflint® H1, and Paraflint® 700-1100 ° F (371-593 ° C) and 1100 ° F + (593 ° C +) distillate fractions of C80 and C105, respectively. The molecular weight distribution (expressed in boiling point) of the wax is briefly shown in Table 3.

Example 2
Preparation of Pt / Beta Catalyst Pt / Beta catalyst was prepared by extruding a water-containing kneaded mixture or paste containing 65 parts zeolite beta and 35 parts alumina (anhydrous base). After drying, the zeolite beta containing the catalyst was calcined under nitrogen at 900 ° F. (482 ° C.) and replaced at ambient temperature with a sufficient amount of ammonium nitrate to remove residual sodium in the zeolite channel. . The extrudate was then washed with deionized water and calcined at 1000 ° F. (538 ° C.) in air. After air calcination, the 65% zeolite beta / 35% alumina extrudate was steamed at 1020 ° F. (549 ° C.) to reduce the alpha value of the calcined catalyst to less than 10. A 65% beta / 35% alumina catalyst with low acidity treated with steam was ion exchanged with a tetraammine platinum chloride solution under ion exchange conditions to uniformly produce a catalyst containing 0.6% Pt. After washing with deionized water to remove residual chloride, the catalyst was dried at 250 ° F. (121 ° C.) followed by a final air calcination at 680 ° F. (360 ° C.).

Example 3
Preparation of Pt / ZSM-48 Catalyst A Pt / ZSM-48 catalyst was prepared by extruding a water-containing kneaded mixture or paste containing 65 parts ZSM-48 and 35 parts alumina (anhydrous base). After drying, the catalyst containing ZSM-48 was calcined at 900 ° F. (482 ° C.) under nitrogen and replaced at ambient temperature with a sufficient amount of ammonium nitrate to remove residual sodium in the zeolite channel. . The extrudate was then washed with deionized water and calcined at 1000 ° F. (538 ° C.) in air. After air calcination, 65% ZSM-48 / 35% alumina catalyst was impregnated in tetraammineplatinum nitrate solution under initial wetting conditions to uniformly produce a catalyst containing 0.6% Pt. Finally, the catalyst was dried at 250 ° F. (121 ° C.) followed by air calcination at 680 ° F. (360 ° C.).

Example 4
Wax hydroprocessing Micro with two three-zone furnaces and two downflow trickle-bed reactors (1/2 inch ID) in cascade (with the option of bypassing the second reactor) The unit was used to conduct wax hydroisomerization experiments. The unit was carefully externally heated to avoid solidification of the high melting C80 wax. In order to reduce the bypass of the raw material and to reduce the pore diffusion resistance of the zeolite, the catalyst extrudate was pulverized to a size of 60 to 80 mesh. Reactors 1 and 2 were then charged with 15 cc of 60-80 mesh Pt / ZSM-48 catalyst and 60-80 mesh Pt / beta catalyst, respectively. Also, 5 cc of 80-120 mesh sand was added to both catalyst beds to fill the void space during catalyst filling. After the unit pressure experiment, the catalyst was dried and reduced at 400 ° F. (204 ° C.) for 1 hour under a hydrogen flow of 1 atm (atm) and 255 cc / min. At the end of this process, the flow of pure hydrogen was stopped and the flow of H ₂ S (2% in hydrogen) was started at 100 cc / min. After H ₂ S breakthrough, reactors 1 and 2 were gradually heated to 700 ° F. (371 ° C.) and maintained at 700 ° F. (371 ° C.) for 1 h (hours). After completion of the presulfidation of the catalyst, the gas stream was switched back to pure hydrogen at a rate of 255 cc / min and the two reactors were cooled.

Cascade Pt / ZSM-48, followed by hydroisomerization of C80 wax on Pt / beta, 1.0 h ⁻¹ LHSV for each catalyst, and 1000 psig (68 atm) and 5500 scf / bbl (979 n. L.L ^-1 ). The wax isomerization experiment was started by first saturating the catalyst bed with feed at 400 ° F. (204 ° C.) and then the reactor was heated to the initial operating temperature. Mass balance was performed overnight for 16-24 h. The reactor temperature was then gradually changed to change the pour point.

The performance of Pt / ZSM-48 alone was evaluated by cooling and bypassing the Pt / beta catalyst in the second reactor. This experiment was performed under the same process conditions used to test the cascade Pt / ZSM-48 and Pt / beta combination (1.0 LHSV, 1000 psig (68 atm), 5500 scf / bbl (979 nL. L ^-1) _H 2), and was carried out following the same procedure.

Example 5
Product Separation and Analysis Off-gas samples were analyzed by GC using a 60 mDB-1 (0.25 mm ID) capillary column equipped with a FID detector. The total liquid product (TLP) was weighed and analyzed by simulated distillation (Simdis such as D2887) using high temperature GC. TLP was distilled into IBP-330 ° F (IBP-166 ° C) naphtha, 330-700 ° F (166-371 ° C) distillate, and 700 ° F + (371 ° C +) lube fraction. To ensure the accuracy of the actual distillation operation, the 700 ° F + (371 ° C +) lube fraction was analyzed once more by Simdis. The pour point and cloud point of 700 ° F + (371 ° C +) lubricant were measured by the D97 and D2500 methods and their viscosities were determined at 40 ° C and 100 ° C according to the D445-3 and D445-5 methods, respectively.

For the isomerization of C80 wax, a plot of lubricant yield versus lubricant pour point on Pt / ZSM-48 followed by Pt / beta catalyst system and Pt / ZSM-48 alone catalyst system. is there. FIG. 2 is a plot of lubricant viscosity vs. lubricant pour point for C80 wax isomerization on Pt / ZSM-48 followed by Pt / beta catalyst system and Pt / ZSM-48 alone catalyst system. For the isomerization of C80 wax, a plot of Viscosity Index (VI) vs. Lubricant Pour Point on Pt / ZSM-48 followed by Pt / Beta catalyst system and Pt / ZSM-48 alone catalyst system. is there. FIG. 4 is a plot of light gas yield versus lubricating oil pour point for C80 wax isomerization on Pt / ZSM-48, followed by Pt / beta catalyst system, and Pt / ZSM-48 alone catalyst system. . FIG. 4 is a plot of naphtha yield versus lubricating oil pour point for C80 wax isomerization on Pt / ZSM-48, followed by Pt / beta catalyst system, and Pt / ZSM-48 alone catalyst system. FIG. 4 is a plot of diesel oil yield versus lubricating oil pour point for C80 wax isomerization on Pt / ZSM-48, followed by Pt / beta catalyst system, and Pt / ZSM-48 alone catalyst system. .

Claims (13)

Substantially free of sulfur or nitrogen, waxes having predominantly hydrocarbon in the range of C ₂₄ -C _110, a conversion method to isoparaffinic lubricant base oil,
First, the wax and the hydrogen co-feed are one-dimensional intermediates having a substantially circular pore structure with an average diameter of 0.50 to 0.65 nm and a difference between the maximum diameter and the minimum diameter of ≦ 0.05 nm. Producing an intermediate product over a one-dimensional molecular sieve catalyst comprising a pore molecular sieve and one or more Group VIII metals; and secondly, said intermediate product is added to zeolite beta And a process for producing an isoparaffinic lubricating base oil through a beta catalyst comprising one or more Group VIII metals. The wax comprises 5% to 80% by weight of 1,100 ° F. + fraction based on its total weight;
The one-dimensional molecular sieve catalyst is maintained at a temperature of 500-800 ° F. (260-427 ° C.);
The beta catalyst is maintained at a temperature of 400-700 ° F. (204-371 ° C.),
The wax is passed over the one-dimensional molecular sieve catalyst at a liquid hourly space velocity of 0.1 to 10 h ⁻¹ ;
The intermediate product is passed over the beta catalyst at a liquid hourly space velocity of 0.1 to 10 h ⁻¹ ;
The method further comprises hydrogen less than 1,500 psig (102 atm), wherein the hydrogen is circulated at 100-10,000 scf / bbl (18-1780 nL L ^-1 ). The conversion method according to claim 1. The one-dimensional molecular sieve catalyst is maintained at a temperature of 600-700 ° F. (316-371 ° C.);
The beta catalyst is maintained at a temperature of 500-600 ° F. (260-316 ° C.),
The wax is passed over the one-dimensional molecular sieve catalyst at a liquid hourly space velocity of 0.5-2 h ⁻¹ ;
The intermediate product is passed over the beta catalyst with a liquid hourly space velocity of 0.5-2 h ⁻¹ ;
The method further comprises less than 1,500 psig (102 atm) of hydrogen, wherein the hydrogen is circulated at 1,000 to 6,000 scf / bbl (178 to 1068 nL L ^-1 ). The conversion method according to claim 2. The Group VIII metal on the catalyst is at least one component selected from the group consisting of Pt and Pd;
The conversion method according to claim 3, wherein the one-dimensional molecular sieve catalyst is ZSM-48 having an alpha value of 10 to 50 before metal introduction. The wax has a 1,000 ° F. + high temperature tail,
The ZSM-48 is filled with 0.5 wt% to 1 wt% Group VIII metal, based on its total weight,
The alpha value of the zeolite beta before filling with the Group VIII metal is less than 15,
The zeolite beta is loaded with 0.5 wt% to 1 wt% Group VIII metal, based on its total weight,
The conversion method according to claim 3, wherein the Group VIII metal is at least one component selected from the group consisting of Pt and Pd. The beta catalyst is Pt / zeolite beta;
The Pt / ZSM-48 and Pt / zeolite beta form a cascade two-bed catalyst system comprising a first bed followed by a second bed, wherein the first bed is Pt / ZSM-48. 6. A conversion process according to claim 5, comprising a catalyst, wherein the second bed comprises a Pt / beta catalyst. The first bed temperature and the second bed temperature are independently controlled;
The intermediate product is cascaded directly to the second bed,
The conversion method according to claim 6.   2. The method of claim 1 having a viscosity index of at least 150 at a lubricating oil pour point of −20 ° C. or a viscosity index of at least 130 at a lubricating oil pour point of −50 ° C. or lower. Isoparaffinic lubricating base oil.   The isoparaffinic lubricating base oil produced by the conversion process according to claim 1, having an aromatic content of less than 1% by weight.   A lubricating oil characterized by having a viscosity index of at least 150 at a lubricating oil pour point of -20 ° C or a viscosity index of at least 130 at a lubricating oil pour point of -50 ° C or lower by the conversion method according to claim 1. .   A lubricating oil characterized by having a viscosity index of at least 150 at a lubricating oil pour point of -20 ° C or a viscosity index of at least 130 at a lubricating oil pour point of -50 ° C or lower by the conversion method according to claim 6. .   The step of passing the wax and intermediate product over the catalyst comprises isoparaffinic having a viscosity index of at least 150 at a lubricating oil pour point of -20 ° C, or a viscosity index of at least 130 at a lubricating oil pour point of -50 ° C or lower. 2. The conversion process according to claim 1, wherein the conversion is carried out under conditions sufficient to produce a lubricating base oil.   The step of passing the wax and intermediate product over the catalyst comprises isoparaffinic having a viscosity index of at least 150 at a lubricating oil pour point of -20 ° C, or a viscosity index of at least 130 at a lubricating oil pour point of -50 ° C or lower. 6. A conversion process according to claim 5, which is carried out under conditions sufficient to produce a lubricating base oil.

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