Lubricant base oil manufacturing method

Abstract

A method for producing a lubricating base oil is provided. (b) separating the feedstream into at least two fraction streams, including a first fraction stream and a second fraction stream; (c) introducing the feedstream before step (b) or the at least two fraction streams after step (b) into a first hydrogenation step; and (d) introducing the feedstream before step (b) or the at least two fraction streams after step (b) into a second hydrogenation step, wherein after steps (b) through (d), the at least two fraction streams produce at least two product streams, including a first product stream and a second product stream, and the first product stream has a higher viscosity index than the second product stream.

Description

[Technical Field]

[0001] The present disclosure relates to a method for making a lubricant base oil. [Background technology]

[0002] Lubricant base oils are the raw materials used to make lubricant products, and generally, good lubricant base oils have a high viscosity index, excellent stability (oxidation, heat, UV, etc.), and low volatility. The American Petroleum Institute (API) classifies lubricant base oils according to their quality as shown in Table 1 below.

[0003] [Table 1]

[0004] The higher the lubricant base oil, the lower the sulfur and nitrogen content, the higher the viscosity index (VI), the lower the pour point, the lower the CCS viscosity, and the lower the Noack volatility. Also, the higher the lubricant base oil, the higher the paraffin content and the lower the naphthene and aromatic content.

[0005] Meanwhile, viscosity index (VI) is one of the important physical properties for evaluating the quality of lubricating base oils. VI is an index related to the change in viscosity with temperature. The higher the VI, the smaller the change in viscosity with temperature. Therefore, lubricating base oils with a high VI have the advantages of being advantageous for engine protection because of their relatively high viscosity at high temperatures and being advantageous for driving engine pumps because of their relatively low viscosity at low temperatures. For these reasons, lubricating base oils with a high viscosity index (VI) are evaluated as higher quality lubricating base oils.

[0006] Due to stricter standards due to environmental regulations and the trend toward lower viscosity and higher quality engine oils, the demand for Group I and II lubricating base oils, which have a high content of impurities and a low viscosity index (VI), is decreasing, while the demand for Group III or higher grade lubricating base oils is increasing. Along these lines, there is also an increasing market demand for lubricating base oils having a viscosity index (VI) that is about 5 to 10 or more higher than that of Group III lubricating base oils (hereinafter referred to as Group III+ lubricating base oils in this disclosure). [Prior art documents] [Patent documents]

[0007] [Patent Document 1] Korean Patent No. 10-2458858 Summary of the Invention [Problem to be solved by the invention]

[0008] The present disclosure aims to provide a method for co-producing conventional and superior quality lubricant base oils from feeds used to produce conventional lubricant base oils. [Means for solving the problem]

[0009] A first aspect of the present disclosure is a method for producing a lubricant base oil, comprising the steps of: (a) providing a feedstream; (b) separating the feedstream into at least two fraction streams, the fraction stream comprising a first fraction stream and a second fraction stream; (c) introducing the feedstream before step (b) or the at least two fraction streams after step (b) into a first hydrogenation step; and (d) introducing the feedstream before step (b) or the at least two fraction streams after step (b) into a second hydrogenation step, wherein after steps (b) through (d), the at least two fraction streams produce at least two product streams, the at least two product streams comprising a first product stream and a second product stream, the first product stream having a higher viscosity index (VI) than the second product stream.

[0010] According to one embodiment, the feedstream comprises vacuum gas oil (VGO), deasphalted oil (DAO), heavy coker gas oil (HCGO), unconverted oil (UCO), distillates thereof, pre-manufactured lubricant base oil, or combinations thereof.

[0011] According to one embodiment, step (b) is carried out by solvent extraction, adsorption, or a combination thereof.

[0012] According to one embodiment, the first hydrogenation step comprises hydrotreating (HDT), hydrocracking (HCK), and combinations thereof.

[0013] According to one embodiment, the second hydrogenation step comprises hydrodewaxing (HDW), hydrofinishing (HDF), and combinations thereof.

[0014] According to one embodiment, the method further comprises the step of (e) fractionally distilling the feed stream or at least two fraction streams.

[0015] According to one embodiment, when the at least two product streams have kinematic viscosities at 100°C of greater than or equal to 2 and less than 4 cSt, a first product stream has a viscosity index (VI) of greater than or equal to 115, and the difference in viscosity index (VI) between the first and second product streams is at least 5.

[0016] According to one embodiment, when the at least two product streams have kinematic viscosities at 100°C of greater than or equal to 4 and less than 8 cSt, a first product stream has a viscosity index (VI) of greater than or equal to 130, and the difference in viscosity index (VI) between the first and second product streams is at least 5.

[0017] A second aspect of the present disclosure is a mineral oil-based lubricating base oil having a kinematic viscosity at 100° C. of 2 or more and less than 4 cSt, and a viscosity index (VI) of 115 or more.

[0018] A third aspect of the present disclosure is a mineral oil-based lubricating base oil having a kinematic viscosity at 100° C. of 4 or more and less than 8 cSt, and a viscosity index (VI) of 130 or more.

[0019] A fourth aspect of the present disclosure is a lubricant composition comprising the mineral lubricating base oil of the second or third aspect. [Effects of the Invention]

[0020] The present disclosure provides a method for simultaneously producing both conventional and superior quality lubricant base oils from feeds for producing conventional lubricant base oils, which is expected to broaden the range of feeds that can produce high-quality lubricant base oils, reduce by-products generated during the production of conventional high-quality lubricant base oils, and reduce feed costs. [Brief explanation of the drawings]

[0021] [Figure 1] 1 is a flowchart outlining a method for producing a lubricating base oil according to an embodiment. [Figure 2]1 is a flowchart outlining a method for producing a lubricating base oil according to an embodiment. [Figure 3] 1 is a flowchart outlining a method for producing a lubricating base oil according to an embodiment. [Figure 4] 1 is a flowchart outlining a method for producing a lubricating base oil according to an embodiment. [Figure 5] 1 is a flowchart outlining a method for producing a lubricating base oil according to an embodiment. [Figure 6] 1 is a flowchart outlining a method for producing a lubricating base oil according to an embodiment. DETAILED DESCRIPTION OF THE INVENTION

[0022] The objects, advantages, and features of the present disclosure will become more apparent from the following detailed description and preferred embodiments in conjunction with the accompanying drawings, but the present disclosure is not necessarily limited thereto. Note that, in describing the present disclosure, if it is determined that a detailed description of related publicly known technologies may unnecessarily obscure the gist of the present disclosure, the detailed description will be omitted.

[0023] The present disclosure provides a method for simultaneously producing a lubricant base oil having a conventional level and a lubricant base oil having a superior quality from a feed for producing a conventional lubricant base oil. The lubricant base oils simultaneously produced by the present disclosure may be a lubricant base oil having a conventional level of VI and a lubricant base oil having a viscosity index (VI) higher than the conventional level.

[0024] Generally, there are two known methods for producing lubricating base oils of higher quality than Group III lubricating base oils. These are i) the production of synthetic base oils (Group IV) using chemical feedstocks, or ii) the production of base oils by hydrotreating crude oils with a high paraffin content. However, in the case of i), the feedstock is more expensive than that of mineral oil-based lubricating base oils, and the amount of feedstock that can be used is small, making production very limited. In addition, in the case of ii), it is difficult to obtain feedstocks with a high paraffin content that can be used as a feed, making it difficult to mass-supply to the market.

[0025] The present disclosure presents an alternative separate from i) and ii). The method of the present disclosure includes a step of providing a feedstream. The feed is not particularly limited as long as it is a feed for producing a lubricant base oil. Preferably, the feed may be a known feed commonly used for producing Group III lubricant base oils. In one embodiment of the present disclosure, the feedstream may include vacuum gas oil (VGO), deasphalted oil (DAO), heavy coker gas oil (HCGO), unconverted oil (UCO), distillates thereof, pre-produced lubricant base oil, or combinations thereof. In the present disclosure, "unconverted oil" refers to unreacted oil that has been supplied to a hydrocracking process for producing fuel oil but has not been subjected to a hydrocracking reaction.

[0026] Illustratively, the feedstream may have the following properties: 80≦VI, S≦3 wt%, N≦1100 ppm, FBP (final boiling point)≦620°C.

[0027] The method of the present disclosure includes a step of separating the feed stream into at least two fraction streams. It should be noted that, in the present disclosure, the separation does not refer to separation of fractions based on differences in boiling points. In other words, the separation step does not include a fractional distillation process for the purpose of separating fractions. Furthermore, in the present disclosure, the separation is a so-called non-reactive separation, which separates the molecules in the feed stream without changing their structure. The separation step of the present disclosure separates the feed stream into a paraffin-rich fraction stream and a paraffin-poor fraction stream. The at least two fraction streams include a first fraction stream and a second fraction stream. In the present disclosure, the nth fraction stream is a fraction stream that is richer in paraffins than the n+1th fraction stream.

[0028] In one embodiment of the present disclosure, the separation step may be performed by solvent extraction, adsorption, or a combination thereof. Separation techniques may include not only solvent extraction and adsorption, but also membrane separation, thermal diffusion, etc. However, in view of ease of separation and excellent yield of the first product stream, it is preferred in the present disclosure that the separation step be performed by solvent extraction or adsorption.

[0029] The solvent extraction can take advantage of the differential solubility of aromatic and non-aromatic components in a feedstream in polar solvents to separate paraffin-rich and paraffin-poor fraction streams.

[0030] The solvent is not particularly limited as long as it is a polar solvent that can separate the feedstream according to paraffin richness without reacting with the components in the feedstream. In one embodiment of the present disclosure, the solvent can include N-methyl-2-pyrrolidone, sulfolane, DMSO (dimethyl sulfoxide), furfural, dimethylacetamide (DMAc), phenol, acetone, aliphatic polyamines, or a combination thereof.

[0031] In one embodiment of the present disclosure, the solvent extraction is carried out at a temperature of about 40 to 120°C, at atmospheric pressure to about 10 kg / cm 2 The solvent extraction may be carried out under a pressure of 0.1 to 1.0 MPa and a volume ratio of solvent to feed stream of 1:1 to 12:1. Optionally, an additional step of removing the solvent used in each of the separated fraction streams may be performed. More specifically, the temperature range of the solvent extraction may be about 40 to 120°C, preferably about 50 to 100°C. The volume ratio of solvent to feed stream may be 1:1 to 12:1, preferably 2:1 to 9:1.

[0032] The adsorption is carried out by injecting an adsorbent into the feedstream, and the adsorbent can selectively adsorb molecules in the feedstream according to the polarity of the molecules. The adsorbent is also not particularly limited as long as it can separate the feedstream based on paraffin richness without reacting with the components in the feedstream. In one embodiment of the present disclosure, the adsorbent can include activated carbon, alumina, clay, silica alumina, zirconia, EU-2, ZSM-5, MCM-4, Molecular Sieve 13X, or a combination thereof. The adsorbent is added to a volume of about 300 ml. 2 The surface area of ​​the cellulose acylate may be 1000 nm or more.

[0033] In one embodiment of the present disclosure, the adsorption may be carried out at a temperature of from room temperature to about 120°C. Of the feed stream, a fraction stream that is not adsorbed by the adsorbent is called a first fraction stream, and a fraction stream that is adsorbed by the adsorbent is called a second fraction stream. The second fraction stream may further be subjected to a desorption step in which it is separated from the adsorbent. In one embodiment of the present disclosure, the desorption may be carried out at a temperature of at least about 200°C. The temperature may be preferably about 200 to 500°C, more preferably about 200 to 400°C.

[0034] In the present disclosure, the separation step can be performed once to produce only the first fraction stream and the second fraction stream, but may also be performed in multiple stages, two or more times, if necessary.

[0035] The method of the present disclosure includes a step of introducing the above-mentioned feed stream or at least two fractional streams into a first hydroprocessing step. The first hydroprocessing step may be carried out before or after the above-mentioned separation step. When the first hydroprocessing step is carried out before the separation step, the feed stream that has been subjected to the first hydroprocessing step is introduced into the separation step. When the first hydroprocessing step is carried out after the separation step, each of the at least two fractional streams produced in the separation step is independently introduced into the first hydroprocessing step.

[0036] In one embodiment of the present disclosure, the first hydrogenation step can include hydrotreating (HDT), hydrocracking (HCK), or a combination thereof. Each of the hydrotreating and hydrocracking steps can be carried out under known process conditions. For example, each of the hydrotreating and hydrocracking steps can be carried out under the respective process conditions applied to conventional Group III lubricant base oil manufacturing processes. Furthermore, when both hydrotreating and hydrocracking are carried out as the first hydrogenation step, the separation step of the present disclosure can be carried out between them.

[0037] In one embodiment of the present disclosure, when the first hydrogenation step is performed before the separation step, the unconverted oil may be supplied as an additional stream after the first hydrogenation step and mixed with the feed stream that has been subjected to the first hydrogenation step. Such a mixed stream may be treated in the same way as the feed stream described below and introduced into the subsequent step.

[0038] The method of the present disclosure includes a step of introducing the above-mentioned feed stream or at least two fraction streams into a second hydrogenation step. The second hydrogenation step is carried out after the first hydrogenation step. The second hydrogenation step may be carried out before or after the above-mentioned separation step. When the second hydrogenation step is carried out before the separation step, the feed stream that has been subjected to the second hydrogenation step is introduced into the separation step. When the second hydrogenation step is carried out after the separation step, each of the at least two fraction streams produced in the separation step is independently introduced into the second hydrogenation step. From the viewpoint of the quality and yield of the final product, the separation step may preferably be carried out before the second hydrogenation step. Here, the before the second hydrogenation step may include the before the first hydrogenation step and all of the area between the after the first hydrogenation step and the before the second hydrogenation step.

[0039] In one embodiment of the present disclosure, the second hydroprocessing step can include hydrodewaxing (HDW), hydrofinishing (HDF), and a combination thereof. Each of the hydrodewaxing and hydrofinishing steps can be carried out under known process conditions. For example, each of the hydrodewaxing and hydrofinishing steps can be carried out under the respective process conditions applied in conventional Group III lubricant base oil manufacturing processes. Furthermore, when both hydrodewaxing and hydrofinishing are carried out as the second hydroprocessing step, the separation step of the present disclosure can be carried out between them.

[0040] In one embodiment of the present disclosure, when the second hydrogenation step is performed before the separation step, a pre-produced lubricant base oil may be supplied as an additional stream after the second hydrogenation step and mixed with the feed stream that has undergone the second hydrogenation step. This mixed stream may be treated in the same manner as the feed stream that has undergone the second hydrogenation step and introduced into the subsequent separation step. The pre-produced lubricant base oil of the present disclosure may include not only lubricant base oils produced by a production line separate from the production method of the present disclosure, but also a portion of the remaining product streams excluding the first product stream produced by the method of the present disclosure. For example, the pre-produced lubricant base oil may be a pre-produced lubricant base oil having the same base oil grade as the second product stream of the present disclosure.

[0041] In one embodiment of the present disclosure, the method may further include a step of fractional distillation (or vacuum distillation) of the feed stream or at least two fraction streams after the first hydrogenation step. The fractional distillation step may be performed before or after each of the second hydrogenation step and the separation step. A distillation feed stream or a distillation fraction stream can be obtained from the feed stream or the fraction stream, respectively, through the fractional distillation step. If necessary, multiple distillation feed streams or multiple distillation fraction streams can be obtained from each of the feed stream or the fraction stream, respectively, through the fractional distillation step, depending on the boiling point (or kinematic viscosity).

[0042] Here, the distillation feed stream and distillation fraction stream refer to unreacted fraction streams that have not undergone reaction in the first hydrogenation step, respectively. The remaining fraction streams other than the distillation feed stream and distillation fraction stream obtained by the fractional distillation step can be used in other subsequent processes, such as a fuel oil production process. For example, the boiling point of the remaining fraction stream may be lower than the boiling point of diesel (about 310°C).

[0043] Flowcharts of various embodiments of the method for producing lubricating base oils according to the present disclosure are shown in Figures 1 to 6, respectively. It should be noted that the embodiments in the accompanying drawings are for illustration and reference purposes only and the scope of the present disclosure is not intended to be limited by the above drawings.

[0044] 1 and 2, a feed stream is first separated into at least two fraction streams, including a first fraction stream and a second fraction stream, through a separation step, and each fraction stream is sequentially subjected to a first hydrogenation step and a second hydrogenation step to produce at least two product streams. The fractional distillation step can be performed after the first hydrogenation step via a VDU (Vacuum Distillation Unit), and can be performed both before and after the second hydrogenation step. As shown in FIG. 2, when the fractional distillation step is performed before the second hydrogenation step, each of the at least two distillation fraction streams, including the first distillation fraction stream and the second distillation fraction stream, can be introduced as a feed for the second hydrogenation step to produce at least two product streams.

[0045] 3 and 4, a feed stream first undergoes a first hydrogenation step and is then separated into at least two fraction streams, including a first fraction stream and a second fraction stream, through a separation step. The at least two fraction streams then undergo a second hydrogenation step to produce at least two product streams. As shown in FIGS. 3 and 4, a fractional distillation step may be performed after the second hydrogenation step or before the separation step. When the fractional distillation step is performed before the separation step or the second hydrogenation step, those skilled in the art will readily recognize that the feed introduced into the separation step or the second hydrogenation step will be converted into a distilled feed stream or a distilled fraction stream, even without further explanation.

[0046] 5 and 6, after the feed stream has undergone the first and second hydrogenation steps, it may be separated into a first and second product stream via a separation step. Again, a fractional distillation step may be performed, and may be performed either before or after the second hydrogenation step.

[0047] As described with reference to Figures 1 to 6, the separation step of the present disclosure may be carried out before the second hydrogenation step or after the second hydrogenation step. However, from the viewpoint of quality control of the final lubricating base oil, the separation step is preferably carried out before the second hydrogenation step. Here, the before the second hydrogenation step may include the before the first hydrogenation step and the entire area between the after the first hydrogenation step and the before the second hydrogenation step.

[0048] The method of the present disclosure produces at least two product streams, including a first product stream and a second product stream, wherein the first product stream is characterized by having a higher VI than the second product stream, and wherein the nth product stream has a higher viscosity index (VI) than the n+1th product stream.

[0049] When a separation step is performed after the second hydrogenation step, as shown in Figures 5 and 6, each of the at least two fraction streams can be at least two product streams. Also, when a fractional distillation step is performed after the second hydrogenation step, as shown in Figure 3, each of the at least two distillation fraction streams can be at least two product streams.

[0050] In one embodiment of the present disclosure, when the kinematic viscosities at 100°C of the at least two product streams are greater than or equal to about 2 and less than 4 cSt, the first product stream can have a viscosity index (VI) of greater than or equal to about 115, such as about 115-150, 115-140, 115-130, 115-125, or 115-120, and the difference in viscosity index (VI) between the first and second product streams is preferably at least about 5, such as about 5-30, 5-20, 5-10, 10-30, or 10-20. In other embodiments, when the at least two product streams have kinematic viscosities at 100°C of about 4 or greater and less than 8 cSt, a first product stream can have a viscosity index (VI) of about 130 or greater, such as about 130-150, 130-145, or 130-140, and the difference in viscosity index (VI) between the first and second product streams is preferably at least about 5, such as about 5-30, 5-20, 5-10, 10-30, or 10-20.

[0051] The second product stream obtained by the process of the present disclosure can have the same lubricant base oil grade as the product obtained by a conventional lubricant base oil manufacturing process in which no separation step is performed.

[0052] In one embodiment of the present disclosure, the content of the first product stream relative to the total product stream may be at least about 10 wt%, such as about 10-90 wt%, about 10-70 wt%, about 10-50 wt%, or about 10-30 wt%. Preferably, the content of the first product stream relative to the total product stream may be at least about 15 wt%, such as about 15-90 wt%, about 15-70 wt%, about 15-50 wt%, or about 15-30 wt%. More preferably, the content of the first product stream relative to the total product stream may be at least about 20 wt%, such as about 20-90 wt%, about 20-70 wt%, about 20-50 wt%, or about 20-30 wt%. More preferably, the content of the first product stream relative to the total product stream may be at least about 25 wt%, such as about 25-90 wt%, about 25-70 wt%, about 25-50 wt%, or about 25-30 wt%.

[0053] The present disclosure provides a mineral oil-based lubricant base oil that can be produced by the above-described process. As an example, the mineral oil-based lubricant base oil can have a kinematic viscosity at 100°C of 2 to less than 4 cSt and a viscosity index (VI) of 115 or greater. As another example, the mineral oil-based lubricant base oil can have a kinematic viscosity at 100°C of 4 to less than 8 cSt and a viscosity index (VI) of 130 or greater.

[0054] The present disclosure also provides a lubricant composition comprising the mineral lubricant base oil described above. In one embodiment of the present disclosure, the lubricant composition comprises at least about 50 wt.%, such as about 50-100 wt.%, about 60-100 wt.%, about 70-100 wt.%, about 80-100 wt.%, about 90-100 wt.%, or about 90-97 wt.% of the mineral lubricant base oil.

[0055] The mineral oil-based lubricating base oil and the lubricant composition containing the same have a higher VI than conventional base oils and lubricant compositions, and are therefore expected to be used as higher quality products.

[0056] Preferred examples are presented below to aid in understanding the present disclosure. However, the following examples are provided merely to facilitate understanding of the present disclosure, and the present disclosure is not limited thereto.

[0057] [Example] The properties of a product (comparative example) obtained by carrying out the lubricant base oil manufacturing process without the "separation step" of the present disclosure were compared with the properties of a first product and a second product obtained by carrying out the lubricant base oil manufacturing process with the "separation step." Solvent extraction and adsorption were used as the separation techniques.

[0058] In the case of solvent extraction, NMP was used as the solvent, and the extraction was carried out under the conditions of a solvent to oil volume ratio of approximately 2:1 to 9:1, extraction temperature of 30 to 90°C, and atmospheric pressure.

[0059] In the case of adsorption, activated carbon was used as the adsorbent, and the adsorption temperature was 60 to 120° C., and the desorption temperature was 200 to 400° C. The results of the comparison of properties are shown in Tables 2 and 3 below.

[0060] [Table 2]

[0061] [Table 3]

[0062] Referring to Tables 2 and 3, it can be seen that the method of the present disclosure can simultaneously produce base oils that maintain conventional grades and base oils that have grades higher than conventional grades. Therefore, it is expected that the present disclosure can provide a new direction for obtaining higher quality lubricant base oils, such as Group III+, by adding a relatively simple non-reactive separation step to the conventional lubricant base oil production process.

[0063] Any simple variations or modifications of the present disclosure should fall within the scope of the present disclosure, and the specific scope of protection of the present disclosure will be made clear by the appended claims.

Claims

1. 1. A method for producing a lubricating base oil, comprising: (a) providing a feed stream; (b) separating the feed stream into at least two fraction streams, including a first fraction stream and a second fraction stream; (c) introducing the feed stream before step (b) or the at least two fraction streams after step (b) into a first hydrogenation step; (d) introducing the feed stream before step (b) or the at least two fraction streams after step (b) into a second hydrogenation step; After steps (b) through (d), the at least two fraction streams produce at least two product streams, including a first product stream and a second product stream, wherein the first product stream has a higher viscosity index (VI) than the second product stream.

2. 10. The method of producing the lubricant base oil of claim 1, wherein the feedstream comprises vacuum gas oil (VGO), deasphalted oil (DAO), heavy coker gas oil (HCGO), unconverted oil (UCO), distillates thereof, pre-made lubricant base oil, or combinations thereof.

3. 10. The method of making the lubricating base oil of claim 1, wherein step (b) is carried out by solvent extraction, adsorption, or a combination thereof.

4. 10. The method of producing the lubricant base oil of claim 1, wherein the first hydrogenation step comprises hydrotreating (HDT), hydrocracking (HCK), and combinations thereof.

5. 10. The method of making the lubricating base oil of claim 1, wherein the second hydrogenation step comprises hydrodewaxing (HDW), hydrofinishing (HDF), and combinations thereof.

6. 10. The method of producing the lubricant base oil of claim 1, further comprising the step of: (e) fractionally distilling the feedstream or at least two fraction streams.

7. 2. The method of producing a lubricant base oil of claim 1, wherein a first product stream has a viscosity index (VI) of 115 or greater and a difference in viscosity index (VI) between the first and second product streams is at least 5, when the at least two product streams have kinematic viscosities at 100° C. of 2 or greater and less than 4 cSt.

8. 2. The method of claim 1, wherein when the at least two product streams have kinematic viscosities at 100° C. of greater than or equal to 4 and less than 8 cSt, a first product stream has a viscosity index (VI) of 130 or greater, and the difference in viscosity index (VI) between the first and second product streams is at least 5.

9. A kinematic viscosity at 100°C of 2 or more and less than 4 cSt, A mineral oil-based lubricating base oil having a viscosity index (VI) of 115 or greater.

10. A kinematic viscosity at 100°C of 4 or more and less than 8 cSt, A mineral oil-based lubricating base oil having a viscosity index (VI) of 130 or greater.

11. A lubricant composition comprising the mineral lubricating base oil of claim 9 or 10.

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