Lubricants with improved oxidation and deposit control properties

Abstract

This invention discloses a method for manufacturing an anti-deposit fluid, the method comprising: combining a base oil with one or more additives to form a blended fluid configured to resist the formation of deposits in an oxidizing environment. The base oil has a viscosity index of at least 80 and a kinematic viscosity of at least 320 cSt at 40°C or at least 14 cSt at 100°C. The base oil comprises greater than or equal to about 90% by weight of a saturated compound, less than or equal to about 10% by weight of an aromatic compound, and at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms.

Description

Technical Field

[0001] Embodiments of the present invention generally relate to fluids such as lubricants made from base oils. Background Technology

[0002] There is a continuous drive to improve the performance of design fluids such as finished lubricants. Exposure to high temperatures in the presence of oxygen, metals, and water typically leads to lubricant oxidation and degradation. Contact with shear forces, as well as extreme high and low temperatures, causes lubricant degradation, rendering it ineffective in managing friction and heat transfer. Machines and components using degraded lubricants operate at suboptimal efficiency and are at risk of damage. Therefore, regular lubricant evacuation and replacement are preferred, typically at predetermined intervals. During this process, users of affected machines suffer productivity losses due to machine downtime and incur costs associated with materials, services, and waste disposal related to lubricant replacement. These harmful aspects are amplified in applications where affected equipment is difficult to access, such as offshore turbines. Summary of the Invention

[0003] In one embodiment, a method of manufacturing an anti-deposit fluid may include combining a base oil with one or more additives to form a blend fluid configured to resist the formation of deposits in an oxidizing environment. The base oil may have a viscosity index of at least 80 and a kinematic viscosity of at least 320 cSt at 40°C or at least 14 cSt at 100°C. The base oil may contain greater than or equal to about 90% by weight of a saturated compound, less than or equal to about 10% by weight of an aromatic compound, and at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms. The base oil may have a T10 distillation point of at least 482°C.

[0004] In another embodiment, a method for reducing deposit formation may include introducing a base oil into a blend. The base oil may have a viscosity index of at least 80 and a kinematic viscosity of at least 320 cSt at 40°C or at least 14 cSt at 100°C. The base oil may contain greater than or equal to about 90% by weight of a saturated compound, less than or equal to about 10% by weight of an aromatic compound, and at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms. The base oil may have a T10 distillation point of at least 482°C. Adding a base oil to a blend can improve the blend's resistance to deposit formation in oxidizing environments.

[0005] In another embodiment, a method for mitigating deposit formation in a device may include introducing a blended fluid into a metallic component of the device. The blended fluid may comprise a base oil and one or more additives. The base oil may have a viscosity index of at least 80 and a kinematic viscosity of at least 320 cSt at 40°C or at least 14 cSt at 100°C. The base oil may comprise greater than or equal to about 90% by weight of a saturated compound, less than or equal to about 10% by weight of an aromatic compound, and at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms. The base oil may have a T10 distillation point of at least 482°C. The blended fluid may be configured to resist deposit formation in an oxidizing environment. Attached Figure Description

[0006] To gain a detailed understanding of the above-described features of the present invention, the invention will be described in more detail with reference to embodiments. Specific aspects of some embodiments are shown in the accompanying drawings. However, it should be noted that the drawings are merely illustrative examples and should not be considered as limiting the scope, and other equally effective embodiments are permitted.

[0007] Figure 1 This is a graph illustrating the comparative test results of the fluid of the present invention and a lubricant blended with high-viscosity Group I base oils, measured according to ASTM D2893 US Steel Oxidation Test, based on one embodiment.

[0008] Figure 2 This is a graph illustrating the comparative test results of the fluid of the present invention and a lubricant blended with high-viscosity Group I base oils, measured according to the Brookfield Viscosity Test (ASTM D2983) according to one embodiment.

[0009] Figure 3 This is a graph showing the comparative test results of the fluid of the present invention and a lubricant blended with high-viscosity Group I base oils, measured according to the ASTM D4684 MRV Apparent Viscosity Test according to one embodiment.

[0010] Figure 4 This is a graph showing the comparative test results of the fluid of the present invention and a lubricant blended with high-viscosity Group I base oils, measured according to an embodiment of the ASTM D5704 L-60-1 Rig Test.

[0011] Figure 5This is a graph illustrating additional comparative test results of the fluid of the present invention and a lubricant blended with a high-viscosity Group I base oil, measured according to an embodiment of the test bench according to ASTM D5704 L-60-1.

[0012] Figure 6 This is a graph illustrating additional comparative test results of the fluid of the present invention and a lubricant blended with a high-viscosity Group I base oil, measured according to an embodiment of the test bench according to ASTM D5704 L-60-1.

[0013] For ease of understanding, the same reference numerals are used where feasible to indicate common elements in the figures. It is conceivable that elements and features of one embodiment may be advantageously incorporated into other embodiments without further description. Detailed Implementation

[0014] Fluids used as lubricants are manufactured by blending one or more base oils with one or more additives. The properties of such fluids, such as viscosity, can be controlled by selecting different base oils and different types and / or quantities of additives. The base oils of this invention can be used to blend fluids with properties superior to other fluids. For example, compared to other fluids, the fluids of this invention can have improved oxidation performance and / or improved low-temperature performance and / or improved deposit control and / or improved heat transfer performance.

[0015] There is a need to improve the design of fluids, particularly lubricants, to enhance their performance at extreme low and high temperatures. It is also beneficial to increase the time interval between continuous lubricant replacements without sacrificing the lubricating properties of the lubricant. This invention relates to fluids blended from base oils comprising high-viscosity Group II base oils, particularly high-viscosity Group II bright oils.

[0016] Base oils are used to manufacture fluids such as automotive lubricants, industrial lubricants, and greases. Base oils are also used in process oils, white oils, metalworking fluids, and heat transfer fluids. Blends of base oils are also called "base oils." Finished lubricants typically contain one or more base oils and additives. Base oil components can be the main components in these finished lubricants and can significantly affect their performance. Generally, a wide range of finished lubricants are manufactured using a few lubricating base oils by varying the mixture of individual base oils and additives.

[0017] According to the American Petroleum Institute (API) classification, base oils are divided into five categories based on their saturated hydrocarbon content (expressed as a weight percentage, wt%), sulfur content (wt%), and viscosity index (see Table 1). Lubricant base oils are typically manufactured on a large scale from petroleum resources. Group I, II, and III base oils are derived from crude oil processed through methods such as solvent extraction, hydrotreating, solvent or catalytic dewaxing, and hydroisomerization. Group III base oils can also be manufactured from synthetic hydrocarbon liquids derived from natural gas, coal, or other fossil resources; Group IV base oils, polyalphaolefins (PAOs), are manufactured through oligomerization of alpha-olefins such as 1-decene; Group V base oils include all substances not belonging to Groups I through IV, such as cycloalkanes, polyalkylene glycols (PAGs), and esters.

[0018] Table 1

[0019]

[0020] Group II base oils may have at least one property that is enhanced relative to the lowest Group II specification. The enhanced property may be, for example, a viscosity index significantly greater than 80 of the Group II specification. Such Group II base oils may have a viscosity index of at least 90, at least 95, at least 100, at least 103, at least 108, or at least 113.

[0021] The Group II high-viscosity base oils of the present invention can have higher viscosity than conventional Group II base oils. The Group II high-viscosity base oils of the present invention can have a kinematic viscosity of at least 14 cSt, at least 20 cSt, at least 25 cSt, at least 30 cSt, or at least 32 cSt at 100°C; and can contain less than 10% by weight of aromatic compounds, more than 90% by weight of saturated compounds, and / or less than 0.03% by weight of sulfur. The saturated compound content can be higher, for example, more than 95% by weight or more than 97% by weight. Such Group II base oils generally appear clear and bright. In at least one embodiment, the Group II base oil has one or more of the following properties: a viscosity index of at least 80, an aromatic compound content of less than 10% by weight, a sulfur content of less than 300 wppm, a kinematic viscosity of at least 14 cSt at 100°C, a kinematic viscosity of at least 320 cSt at 40°C, a pour point of -9°C or less, and / or a cloud point of -2°C or less. In at least one embodiment, the Group II base oil has a viscosity index of at least 95 and / or a kinematic viscosity of 30 cSt to 40 cSt at 100°C. The Group II base oil of the present invention may have a pour point of -10°C or less, for example -20°C or less or -25°C to -30°C. The Group II base oil of the present invention may have a T10 distillation point of at least 482°C.

[0022] Group II base oils with a kinematic viscosity of 29 to 32 cSt or greater at 100°C are advantageous in reducing or minimizing the use of thickening additives, for example, in specific applications where such base oils can be used as alternatives to conventional Group I bright oils. Furthermore, or alternatively, Group II base oils with a kinematic viscosity of 29 to 32 cSt or greater at 100°C can be advantageous in applications where Group I bright oils may be unsuitable, such as in environments where Group I bright oils have difficulty with oxidative stability.

[0023] The Group II high-viscosity base oils of this invention can be derived from low-severity deasphalting of residual oil fractions to form deasphalted oils. The deasphalted oils can be demetallized, hydrotreated, hydrocracking, hydrodewaxing, and hydrorefined to prepare high-saturated compound base oils with a viscosity range similar to conventional Group I bright oils. However, the resulting base oils may be Group II high-viscosity base oils with improved color, lower pour point, equal or higher viscosity index, and higher saturated compound content than Group I bright oils.

[0024] In at least one embodiment, the Group II base oil has a kinematic viscosity of about 480 cSt at 40°C, a kinematic viscosity of about 33 cSt at 100°C, a viscosity index of about 100, an emulsification time of about 15 minutes at 82°C, a pour point of about -21°C, and a saturated compound content of about 99% by weight. Table 2 provides a comparison of the properties of the Group II base oils in the examples with typical values ​​for Group I bright oils.

[0025] Table 2

[0026]

[0027] Therefore, the Type II high-viscosity base oil of the present invention can be used in lubricant blends as a substitute for existing Type I bright oils.

[0028] Overview of Group II Base Oils

[0029] Group II lubricant base oils, including Group II bright oils, can be produced from low-severity C... 4+The deasphalted oil produced from deasphalting is used to manufacture the product. As used herein, low-severity deasphalting refers to deasphalting under conditions that result in a high deasphalted oil yield (and / or a reduced amount of waste asphalt or residual oil), said high deasphalted oil yield being, for example, at least 50% by weight, at least 55% by weight, at least 60% by weight, at least 65% by weight, at least 70% by weight, or at least 75% by weight of the deasphalted feed. Group I base oils (including bright oils) can be formed without solvent extraction of the deasphalted oil. Group II base oils (including bright oils) can be formed using a combination of catalytic and solvent processing. Compared to conventional bright oils manufactured from deasphalted oil formed under low-severity conditions, the Group I and Group II bright oils of this invention are substantially hazy-free after long-term storage.

[0030] In other aspects, methods for catalytically processing C3 deasphalted oil to form Group II bright oils are provided. Catalytic processing to form Group II bright oils can provide bright oils with improved compositional properties.

[0031] Crude oil is typically described as containing multiple boiling ranges. Lower-boiling-range compounds in crude oil correspond to naphtha or kerosene fuels. Medium-boiling-range distillate compounds can be used as diesel fuel or lubricant base oils. If any higher-boiling-range compounds are present in crude oil, these are considered residual or "residue" compounds, corresponding to the portion of crude oil remaining after atmospheric and / or vacuum distillation.

[0032] In some processing methods, residual oil fractions can be deasphalted, with the deasphalted oil used as part of the feedstock for forming lubricant base oils. The deasphalted oil used as feedstock for forming lubricant base oils is manufactured using propane deasphalting. This propane deasphalting corresponds to “high-severity” deasphalting, as indicated by a typical yield of deasphalted oil relative to the initial residual oil fraction of about 40% by weight or less, typically 30% by weight or less. In a typical lubricant base oil manufacturing process, the deasphalted oil can then undergo solvent extraction to reduce the aromatic content, followed by solvent dewaxing to form the base oil. The low yield of deasphalted oil is partly due to the fact that conventional methods cannot produce lubricant base oils that do not develop haze over time from lower-severity deasphalting.

[0033] In some respects, it has been found that using a mixture of catalytic processing such as hydrotreating and solvent processing such as solvent dewaxing can enable the production of lubricant base oils from deasphalted oils while simultaneously producing base oils that exhibit little or no haze over extended periods. Deasphalted oils can be used by employing C4 solvents, C5 solvents, and C... 6+ Solvent, two or more C 4+ A mixture of solvents or two or more C 5+The deasphalting process is used to manufacture a mixture of solvents. The deasphalting process can also correspond to the following deasphalting oil yield process: the deasphalting oil yield process has a deasphalting oil yield of at least 50% by weight, or at least 60% by weight, or at least 65% by weight, or at least 70% by weight, or at least 75% by weight for vacuum residue feed having a T10 distillation point of at least 400°C or at least 510°C. It is believed that the reduced haze formation is partly due to the reduction or minimization of the difference between the pour point and cloud point of the base oil and / or partly due to the formation of bright oils with a cloud point of -2°C or less or -5°C or less.

[0034] For the manufacture of Group II base oils, in some aspects, the deasphalted oil can be hydrotreated (hydrocracking and / or hydrocracking) to achieve a conversion of 10% to 40% by weight at approximately 700℉+ (370℃+). The effluent from the hydrotreated operation can be fractionated to separate the lower boiling point portion from the boiling range portion of the lubricant base oil. The boiling range portion of the lubricant can then be hydrocracking, dewaxing, and hydrorefining to produce a catalytically dewaxed effluent. In some embodiments, the boiling range portion of the lubricant can be incompletely dewaxed, such that the wax content of the heavier portion or potentially bright oil portion of the catalytically dewaxed effluent is at least 6% by weight, at least 8% by weight, or at least 10% by weight. This incomplete dewaxing can also be applied to the formation of light, medium, or heavy neutral lubricant base oils that do not require further solvent upgrading to form a fog-free base oil. In this discussion, the heavier portion / potential bright oil portion can roughly correspond to the 538℃+ portion of the dewaxed effluent. The heavier fraction of the effluent after catalytic dewaxing can then be solvent-treated by solvent dewaxing to form a solvent-dewaxed effluent. The solvent-dewaxed effluent can be separated to form a variety of base oils, including at least a portion of Group II bright oil products, that exhibit a decreasing (e.g., no) tendency to develop haze over time.

[0035] For the production of Group II base oils, in other respects, the deasphalted oil can be hydrotreated (hydrocracking and / or hydrocracking) to achieve a conversion of at least 40% by weight or at least 50% by weight at 370°C+. The effluent from the hydrotreatment operation can be fractionated to separate the lower boiling point fraction from the boiling range fraction of the lubricant base oil. The boiling range fraction of the lubricant base oil can then be hydrocracking, dewaxing, and hydrorefining to produce a catalytically dewaxed effluent. The catalytically dewaxed effluent can then be solvent-extracted to form a raffinate. The raffinate can be separated to form a variety of base oils with a decreasing (e.g., no) tendency to form haze over time, including at least a portion of Group II bright oil products. In yet another respect, the Group II bright oil products can be formed without further solvent treatment after catalytic dewaxing.

[0036] In other respects, it has been found that catalytic treatment can be used to process C3, C4, C5 and / or C64 carbon atoms. 5+ The deasphalted oil is used to produce Group II bright oils with improved compositional properties. The deasphalted oil can be hydrotreated to reduce the content of heteroatoms (e.g., sulfur and nitrogen), followed by catalytic dewaxing under low-sulfur conditions. In some embodiments, hydrocracking can be included as part of an acid hydrotreatment stage and / or as part of a low-sulfur dewaxing stage.

[0037] In various aspects, multiple combinations of catalytic and / or solvent processing can be used for lubricant base oils formed from deasphalted oils, including Group II bright oils. These combinations include, but are not limited to:

[0038] a) Hydrotreating of deasphalted oil under acidic conditions (i.e., a sulfur content of at least 500 w ppm); separation of the effluent from the hydrotreating operation to form at least a lubricant boiling range fraction, and solvent dewaxing of the lubricant boiling range fraction. In some aspects, the hydrotreating operation of deasphalted oil can correspond to hydrotreating, hydrocracking, or a combination thereof.

[0039] b) Hydrotreating the deasphalted oil under acidic conditions (i.e., a sulfur content of at least 500 w ppm); separating the effluent from the hydrotreating operation to form at least a lubricant boiling range fraction; and catalytically dewaxing the lubricant boiling range fraction under low-sulfur conditions (i.e., 500 w ppm or less sulfur). Catalytic dewaxing may correspond to catalytic dewaxing using a dewaxing catalyst with a pore size greater than 8.4 Å. In some embodiments, the low-sulfur processing conditions may further include hydrocracking, precious metal hydrotreating, and / or hydrorefining. Optional hydrocracking, precious metal hydrotreating, and / or hydrorefining may be performed before and / or after catalytic dewaxing. For example, the sequence of catalytic processing under low-sulfur conditions may be precious metal hydrotreating, followed by hydrocracking, and then catalytic dewaxing.

[0040] c) The process described in b) above, followed by additional separation of at least a portion of the catalytically dewaxed effluent. This additional separation can correspond to solvent dewaxing, solvent extraction (e.g., solvent extraction with furfural or n-methylpyrrolidone), physical separation such as ultracentrifugation, or a combination thereof.

[0041] d) The process described in a) above is followed by catalytic dewaxing of at least a portion of the solvent dewaxing product (under low-sulfur conditions). In some embodiments, the low-sulfur processing conditions may further include hydrotreating (e.g., precious metal hydrotreating), hydrocracking, and / or hydrorefining. Additional low-sulfur hydrotreating operations may be performed before and / or after catalytic dewaxing.

[0042] In the following discussion, a stage can correspond to a single reactor or multiple reactors. In some embodiments, multiple parallel reactors can be used to perform one or more processes, or multiple parallel reactors can be used for all processes in a single stage. Each stage and / or reactor can contain one or more catalyst beds containing a hydrocracking catalyst. It should be noted that the term "catalyst bed" in the following discussion can refer to a partially physical catalyst bed. For example, the catalyst bed within a reactor can be partially filled with a hydrocracking catalyst and partially filled with a dewaxing catalyst. For ease of description, even though both catalysts can be stacked together in a single catalyst bed, the hydrocracking catalyst and the dewaxing catalyst can conceptually be referred to as separate catalyst beds.

[0043] In this discussion, conditions can be provided for various types of hydrogenation operations for feed or effluent. Examples of hydrogenation operations include, but are not limited to, one or more of hydrotreatment, hydrocracking, catalytic dewaxing, and hydrorefining / aromatic saturation. By using at least one controller, or multiple controllers, to control one or more hydrogenation operation conditions, these conditions can be controlled to achieve desired values ​​for conditions (e.g., temperature, pressure, liquid hourly space velocity, process gas rate). In some aspects, for a given type of hydrogenation operation, at least one controller can be associated with each type of hydrogenation operation condition. In some aspects, one or more hydrogenation operation conditions can be controlled by an associated controller. Examples of structures controllable by a controller include, but are not limited to: valves controlling flow rate, pressure, or combinations thereof; heat exchangers and / or heaters controlling temperature; and one or more flow meters and one or more associated valves controlling the relative flow rates of at least two flows. Such a controller may include a controller feedback loop containing at least one processor, a detector for detecting the value of a controlled variable (e.g., temperature, pressure, flow rate), and a processor output for controlling the value of manipulated variables (e.g., changing valve position, increasing or decreasing duty cycle, and / or heater temperature). In some implementations, at least one hydrogenation operation condition for a given type of hydrogenation operation may not have an associated controller.

[0044] In this discussion, unless otherwise stated, lubricant boiling range fractions correspond to fractions having an initial boiling point of at least about 370°C (about 700°F) or, alternatively, a T5 boiling point. Distillate fuel boiling range fractions, such as diesel product fractions, correspond to fractions with a boiling range of about 193°C (375°F) to about 370°C (about 700°F). Thus, distillate fuel boiling range fractions (e.g., distillate fuel product fractions) can have an initial boiling point of at least about 193°C (or, alternatively, a T5 boiling point) and a final boiling point of about 370°C or less (or, alternatively, a T95 boiling point). Naphtha boiling range fractions correspond to fractions with a boiling range of about 36°C (122°F) to about 193°C (375°F) to about 370°C (about 700°F). Therefore, naphtha fuel product fractions can have an initial boiling point of at least about 36°C (or alternatively, a T5 boiling point) and a final boiling point of about 193°C or less (or alternatively, a T95 boiling point). It is worth noting that 36°C roughly corresponds to the boiling points of various isomers of C5 alkanes. Fuel boiling range fractions can correspond to distillate fuel boiling range fractions, naphtha boiling range fractions, or fractions containing both distillate fuel boiling range and naphtha boiling range components. Light fractions are defined as products with boiling points below about 36°C, which include various C1-C4 compounds. When determining the boiling point or boiling range of a feed or product fraction, appropriate ASTM test methods can be used, such as the procedures described in ASTM D2887, D2892, and / or D86. Preferably, ASTM D2887 should be used unless the sample is not suitable for characterization according to ASTM D2887. For example, for samples that will not be completely eluted from the column, ASTM D7169 can be used.

[0045] Feeding

[0046] In all respects, at least a portion of the feed used for the processing described herein can correspond to a vacuum residue fraction or another type of 950℉+ (510℃+) or 1000℉+ (538℃+) fraction. Another example of a method for forming a 950℉+ (510℃+) or 1000℉+ (538℃+) fraction is high-temperature flash separation. The 950℉+ (510℃+) or 1000℉+ (538℃+) fraction formed by high-temperature flash separation can be processed in a manner similar to that of vacuum residue.

[0047] Vacuum residue fractions or 950℉+ (510℃+) fractions formed by another process (e.g., flash fractionation of oil residues or bituminous fractions) can be deasphalted at low harshness to form deasphalted oil. In some embodiments, the feed may also include a portion of conventional feedstock for the manufacture of lubricant base oils, such as vacuum gas oil.

[0048] Vacuum residue (or other 510°C+) fractions can correspond to fractions having a T5 distillation point (ASTM D2892; or ASTM D7169, if the fraction is not completely eluted from the chromatographic system) of at least about 900°F (482°C), at least 950°F (510°C), or at least 1000°F (538°C). Alternatively, vacuum residue fractions can be characterized based on a T10 distillation point (ASTM D2892 / D7169) of at least about 900°F (482°C), at least 950°F (510°C), or at least 1000°F (538°C).

[0049] The metal content of residue oil (or other 510°C+) fractions can be very high. For example, the total content of nickel, vanadium, and iron in residue oil fractions can be very high. In one respect, each gram of residue oil can contain at least 0.00005 grams of Ni / V / Fe (50 wppm) or at least 0.0002 grams of Ni / V / Fe (200 wppm) in total elemental composition of nickel, vanadium, and iron. In other respects, heavy oil can contain at least 500 wppm of nickel, vanadium, and iron, for example, up to 1000 wppm or more.

[0050] Contaminants such as nitrogen and sulfur are commonly found in residue oil (or other 510°C+) fractions, typically in organically bound forms. Based on the total weight of the residue oil fraction, the nitrogen content can range from approximately 50 Wppm to approximately 10,000 Wppm of elemental nitrogen or more. Based on the total weight of the residue oil fraction, the sulfur content can range from 500 Wppm to 100,000 Wppm of elemental sulfur or more, or from 1,000 Wppm to 50,000 Wppm, or from 1,000 Wppm to 30,000 Wppm.

[0051] Another method for characterizing residue (or other 510°C+) fractions is based on the COC (Chemical Carbon Residue) of the feed. The COC of the residue fraction can be at least about 5% by weight, for example at least about 10% by weight or at least about 20% by weight. Alternatively or alternatively, the COC of the residue fraction can be about 50% by weight or less, for example about 40% by weight or less or about 30% by weight or less.

[0052] In some respects, vacuum gas oil fractions can be co-processed with deasphalted oil. Vacuum gas oil can be combined with deasphalted oil in various amounts, from 20 parts (by weight) of deasphalted oil to 1 part of vacuum gas oil (i.e., 20:1) to 1 part of deasphalted oil to 1 part of vacuum gas oil. In some respects, the ratio of deasphalted oil to vacuum gas oil can be at least 1:1 (by weight), at least 1.5:1, or at least 2:1. Typical (vacuum) gas oil fractions can include, for example, T5 to T95 distillation points of 650℉ to 1050℉ (343℃ to 566℃), or 650℉ to 1000℉ (343℃ to 538℃), or 650℉ to 950℉ (343℃ to 510℃), or 650℉ to 900℉ (343℃ to 482℃), or approximately 700℉ to 1050℉ (370℃ to 566℃), or approximately 700℉ to 1050℉ (370℃ to 566℃). Fractions of about 00℉ (370℃ to 538℃), or about 700℉ to 950℉ (370℃ to 510℃), or about 700℉ to 900℉ (370℃ to 482℃), or 750℉ to 1050℉ (399℃ to 566℃), or 750℉ to 1000℉ (399℃ to 538℃), or 750℉ to 950℉ (399℃ to 510℃), or 750℉ to 900℉ (399℃ to 482℃). For example, a suitable vacuum gas oil fraction can have a T5 distillation point of at least 343°C and a T95 distillation point of 566°C or less; or a T10 distillation point of at least 343°C and a T90 distillation point of 566°C or less; or a T5 distillation point of at least 370°C and a T95 distillation point of 566°C or less; or a T5 distillation point of at least 343°C and a T95 distillation point of 538°C or less.

[0053] Solvent deasphalting

[0054] Solvent deasphalting is a solvent extraction process. In some respects, suitable solvents for the methods described herein include alkanes or other hydrocarbons (e.g., alkenes) containing 4 to 7 carbons per molecule. Examples of suitable solvents include n-butane, isobutane, n-pentane, and C64. 4+ Alkanes, C 5+ Alkanes, C 4+ Hydrocarbons and C 5+ Hydrocarbons. In other respects, suitable solvents can include C3 hydrocarbons, such as propane. Examples of suitable solvents in this other respect include propane, n-butane, isobutane, n-pentane, and C3 hydrocarbons. 3+ Alkanes, C 4+ Alkanes, C 5+ Alkanes, C 3+ Hydrocarbons, C 4+ Hydrocarbons and C 5+ hydrocarbon.

[0055] This discussion will include C nA solvent for hydrocarbons is defined as a solvent containing at least 80% by weight, or at least 85% by weight, or at least 90% by weight, or at least 95% by weight, or at least 98% by weight of an alkane having n carbon atoms. Similarly, a solvent containing C... n+ A solvent for hydrocarbons is defined as a solvent containing at least 80% by weight, or at least 85% by weight, or at least 90% by weight, or at least 95% by weight, or at least 98% by weight of an alkane having n or more carbon atoms.

[0056] This discussion will include C n Solvents for alkanes (hydrocarbons) are defined as including cases where the solvent corresponds to a single alkane (hydrocarbon) containing n carbon atoms (e.g., n = 3, 4, 5, 6, 7) and cases where the solvent comprises a mixture of alkanes (hydrocarbons) containing n carbon atoms. Similarly, solvents containing C... n+ Solvents for alkanes (hydrocarbons) are defined as including cases where the solvent corresponds to a single alkane (hydrocarbon) containing n or more carbon atoms (e.g., n = 3, 4, 5, 6, 7) and cases where the solvent corresponds to a mixture of alkanes (hydrocarbons) containing n or more carbon atoms. Therefore, [the solvent] containing C... 4+ Solvents for alkanes can correspond to: solvents containing n-butane; solvents containing n-butane and isobutane; solvents corresponding to mixtures of one or more butane isomers and one or more pentane isomers; or any other convenient combination of alkanes containing four or more carbon atoms. Similarly, solvents containing C 5+ Solvents for alkanes (hydrocarbons) are defined as solvents corresponding to a single alkane (hydrocarbon) or solvents corresponding to a mixture of alkanes (hydrocarbons) containing five or more carbon atoms. Alternatively, other types of solvents may also be suitable, such as supercritical fluids. In all respects, solvents used for solvent deasphalting can be substantially composed of hydrocarbons, such that at least 98% by weight or at least 99% by weight of the solvent corresponds to a compound containing only carbon and hydrogen. In this case, the deasphalting solvent corresponds to C... 4+ Regarding deasphalting solvents, C 4+ The deasphalting solvent may contain less than 15% by weight, less than 10% by weight, or less than 5% by weight of propane and / or other C3 hydrocarbons, or C4 hydrocarbons. 4+ The deasphalting solvent is substantially free of propane and / or other C3 hydrocarbons (less than 1% by weight). In deasphalting solvents corresponding to C... 5+ Regarding deasphalting solvents, C 5+ The deasphalting solvent may contain less than 15% by weight, less than 10% by weight, or less than 5% by weight of propane, butane, and / or other C3-C4 hydrocarbons, or C4 hydrocarbons. 5+The deasphalting solvent is substantially free of propane, butane, and / or other C3-C4 hydrocarbons (less than 1% by weight). In the deasphalting solvent corresponding to C... 3+ Regarding deasphalting solvents, C 3+ The deasphalting solvent may contain less than 10% by weight or less than 5% by weight of ethane and / or other C2 hydrocarbons, or C4 hydrocarbons. 3+ The deasphalting solvent is substantially free of ethane and / or other C2 hydrocarbons (less than 1% by weight).

[0057] Deasphalting of heavy hydrocarbons, such as vacuum residue, is known in the art and is commercially practiced. Deasphalting processes typically involve contacting heavy hydrocarbons with alkane solvents (propane, butane, pentane, hexane, heptane, etc., and their isomers) in pure or mixed form to produce two types of product streams. One type of product stream can be deasphalted oil extracted via alkane extraction, which is then further separated to produce a deasphalted oil stream. The second type of product stream can be the residual portion of the feed that is insoluble in solvents, commonly referred to as residual oil or asphaltenes. The deasphalted oil fraction can be further processed into fuels or lubricants. The residual oil fraction can be further used as a blending component to produce asphalt, fuel oil, and / or other products. The residual oil fraction can also be used as feed for gasification processes such as partial oxidation, fluidized bed combustion, or coking processes. The residual oil can be delivered to these processes as a liquid (with or without additional components) or as a solid (particulate or lumpy) form.

[0058] During solvent deasphalting, a residual oil boiling range feed (optionally also including a portion of vacuum gas oil feed) can be mixed with a solvent. The solvent-soluble portion of the feed is then extracted, leaving a residue that is barely soluble or insoluble in the solvent. The deasphalted feed fraction extracted with solvent is commonly referred to as deasphalted oil. Typical solvent deasphalting conditions involve mixing the feed fraction with the solvent at a weight ratio of about 1:2 to about 1:10, for example, about 1:8 or less. Typical solvent deasphalting temperatures range from 40°C to 200°C or from 40°C to 150°C, depending on the nature of the feed and solvent. Pressures during solvent deasphalting can range from about 50 psig (345 kPag) to about 500 psig (3447 kPag).

[0059] It should be noted that the above solvent deasphalting conditions represent a general range, and the conditions will vary depending on the feed. For example, under typical deasphalting conditions, increasing the temperature often increases the quality of the resulting deasphalted oil while decreasing the yield. Under typical deasphalting conditions, increasing the molecular weight of the solvent often decreases the quality of the resulting deasphalted oil while increasing the yield, because other compounds in the residue fraction can be soluble in solvents containing higher molecular weight hydrocarbons. Under typical deasphalting conditions, increasing the amount of solvent often increases the yield of the resulting deasphalted oil. As those skilled in the art will understand, the specific feed conditions can be selected based on the yield of the deasphalted oil obtained from solvent deasphalting. In the case of using C3 deasphalting solvent, the solvent deasphalting yield can be 40% by weight or less. In some aspects, C4 deasphalting can be carried out with a deasphalted oil yield of 50% by weight or less or 40% by weight or less. In various aspects, the deasphalted oil yield derived from C3 deasphalting solvents can be increased. 4+ The yield of deasphalted oil from solvent deasphalting can be at least 50% by weight, at least 55% by weight, at least 60% by weight, at least 65% by weight, or at least 70% by weight relative to the weight of the deasphalting feed. In cases where the deasphalting feed includes a vacuum gas oil portion, the yield from solvent deasphalting can be characterized based on the weight of the 950℉+ (510℃) portion of the deasphalted oil relative to the weight of the 510℃+ portion of the feed. When using C... 4+ Regarding these aspects of the solvent, the yield of deasphalted oil from solvent deasphalting at 510°C+ relative to the weight of the 510°C+ portion of the deasphalted feed can be at least 40% by weight, at least 50% by weight, at least 55% by weight, at least 60% by weight, at least 65% by weight, or at least 70% by weight. When using C... 4+ Regarding these aspects of the solvent, the yield of the 510°C+ deasphalted oil from solvent deasphalting relative to the weight of the 510°C+ portion of the deasphalted feed can be 50% by weight or less, or 40% by weight or less, or 35% by weight or less.

[0060] Hydrotreating and hydrocracking

[0061] Following deasphalting, the deasphalted oil (and any other fractions combined with it) can be further processed to form lubricant base oils. This can include hydrotreating and / or hydrocracking to remove heteroatoms to desired levels, reduce the Kangerh carbon content, and / or provide an increase in viscosity index (VI). According to these aspects, the deasphalted oil can be hydrotreated by hydrotreating, hydrocracking, or a combination of both.

[0062] Deasphalted oil can be hydrotreated and / or hydrocracking under conditions of little or no solvent extraction before and / or after deasphalting. As a result, the deasphalted oil feedstock for hydrotreatment and / or hydrocracking can contain a significant amount of aromatic compounds. In various aspects, the aromatic compound content of the deasphalted oil feedstock can be at least 50% by weight, or at least 55% by weight, or at least 60% by weight, or at least 65% by weight, or at least 70% by weight, or at least 75% by weight, for example, up to 90% by weight or more. Alternatively or additionally, the saturated compound content of the deasphalted oil feedstock can be 50% by weight or less, or 45% by weight or less, or 40% by weight or less, or 35% by weight or less, or 30% by weight or less, or 25% by weight or less, for example, as low as 10% by weight or less. In this discussion and claims, the aromatic compound content and / or saturated compound content of the fraction can be determined according to ASTM D7419.

[0063] The reaction conditions in the demetallization and / or hydrotreating and / or hydrocracking processes of the deasphalted oil (and optionally co-feed with vacuum gas oil) can be selected to produce a desired level of feed conversion. Any convenient type of reactor can be used, such as a fixed-bed (e.g., trickle-bed) reactor. Feed conversion can be defined based on the conversion of molecules with boiling points above a temperature threshold to molecules with boiling points below that threshold. The conversion temperature can be any convenient temperature, such as approximately 700℉ (370°C) or 1050℉ (566°C). The conversion amount can correspond to the total molecular conversion in the combined hydrotreating and hydrocracking stages used for the deasphalted oil. A suitable amount of molecule with a boiling point above 1050℉ (566℃) to convert to molecule with a boiling point below 566℃ comprises a conversion rate of 30% to 90% by weight, or 30% to 80% by weight, or 30% to 70% by weight, or 40% to 90% by weight, or 40% to 80% by weight, or 40% to 70% by weight, or 50% to 90% by weight, or 50% to 80% by weight, or 50% to 70% by weight, relative to 566℃. Specifically, the conversion amount relative to 566℃ can be 30% to 90% by weight, or 30% to 70% by weight, or 50% to 90% by weight. Alternatively or concurrently, a suitable amount of molecules with boiling points above about 700℉ (370℃) to be converted to molecules with boiling points below 370℃ comprises a conversion rate of 10% to 70% by weight, or 10% to 60% by weight, or 10% to 50% by weight, or 20% to 70% by weight, or 20% to 60% by weight, or 20% to 50% by weight, or 30% to 70% by weight, or 30% to 60% by weight, or 30% to 50% by weight, relative to 370℃. Specifically, the conversion amount relative to 370℃ can be 10% to 70% by weight, or 20% to 50% by weight, or 30% to 60% by weight.

[0064] Deasphalted oils produced through hydrotreating can also be characterized based on product quality. Following hydrotreating (hydroprocessing and / or hydrocracking), the sulfur content of hydrotreated deasphalted oils can be 200 wppm or less, or 100 wppm or less, or 50 wppm or less (e.g., as low as approximately 0 wppm). Alternatively or alternatively, the nitrogen content of hydrotreated deasphalted oils can be 200 wppm or less, or 100 wppm or less, or 50 wppm or less (e.g., as low as approximately 0 wppm). Alternatively or alternatively, the Concorde carbon residue of hydrotreated deasphalted oils can be 1.5 wt% or less, or 1.0 wt% or less, or 0.7 wt% or less, or 0.1 wt% or less, or 0.02 wt% or less (e.g., as low as approximately 0 wt%). Concorde carbon residue can be determined according to ASTM D4530.

[0065] In various aspects, the feed can be contacted with a demetallization catalyst before contacting the hydrotreating catalyst. The metal concentration (Ni+V+Fe) of the deasphalted oil can be on the order of 10 to 100 wppm. Contacting a conventional hydrotreating catalyst with a metal content of 10 wppm or greater can cause the catalyst to deactivate at a faster rate than is expected in commercial settings. Contacting the metal-containing feed with a demetallization catalyst before the hydrotreating catalyst allows at least a portion of the metal to be removed by the demetallization catalyst, which can reduce or minimize the deactivation of the hydrotreating catalyst and / or other subsequent catalysts in the process flow. Commercially available demetallization catalysts can be suitable, such as macroporous amorphous oxide catalysts, which may contain Group VI and / or Group VIII non-noble metals to provide some hydrotreating activity.

[0066] In all aspects, deasphalted oil can be contacted with a hydrotreating catalyst under effective hydrotreating conditions. The catalysts used can include conventional hydrotreating catalysts, such as those containing at least one Group VIII non-noble metal (columns 8-10 of the IUPAC periodic table) such as Fe, Co, and / or Ni; and at least one Group VI metal (column 6 of the IUPAC periodic table) such as Mo and / or W. Such hydrotreating catalysts may comprise transition metal sulfides impregnated or dispersed on a refractory support or substrate such as alumina and / or silica. The support or substrate itself typically has no apparent / measurable catalytic activity. Catalysts that are substantially free of support or substrate, often referred to as bulk catalysts, typically exhibit higher volumetric activity than their supported counterparts.

[0067] The catalyst can be in bulk or supported form. Besides alumina and / or silica, other suitable support / support materials can include, but are not limited to, zeolites, titanium dioxide, silica-titanium dioxide, and titanium dioxide-alumina. Suitable alumina is porous alumina, for example, with an average pore size of 50 μm. or 75 to Surface area of ​​100 to 300 m² 2 / g or 150 to 250 mg 2 / g and pore volume of 0.25 to 1.0 cm³ 3 / g or 0.35 to 0.8cm 3 / g of γ or η alumina. More generally, any suitable size, shape, and / or pore size distribution of catalyst suitable for hydrotreating distillates (including lubricant base oils) in a conventional manner with boiling range feedstocks can be used. For example, the support or carrier material is an amorphous support, such as a refractory oxide. For example, the support or carrier material can be free of or substantially free of molecular sieves, where substantially free of molecular sieves is defined as a molecular sieve content of less than about 0.01% by weight.

[0068] At least one Group VIII non-noble metal in oxide form can typically be present in amounts ranging from about 2 wt% to about 40 wt%, for example, from about 4 wt% to about 15 wt%. At least one Group VI metal in oxide form can typically be present in amounts ranging from about 2 wt% to about 70 wt%, for example, in supported catalysts, from about 6 wt% to about 40 wt% or from about 10 wt% to about 30 wt%. These weight percentages are based on the total weight of the catalyst. Suitable metal catalysts include cobalt / molybdenum (1 to 10% Co in oxide form, 10 to 40% Mo in oxide form), nickel / molybdenum (1 to 10% Ni in oxide form, 10 to 40% Co in oxide form), or nickel / tungsten (1 to 10% Ni in oxide form, 10 to 40% W in oxide form) on alumina, silica, silica-alumina, or titanium dioxide.

[0069] Hydrogenation is carried out in the presence of hydrogen. Therefore, a hydrogen stream is fed or injected into the container, reaction zone, or hydrogenation operation zone containing the hydrogenation catalyst. Hydrogen contained in a hydrogen "processing gas" is supplied to the reaction zone. The processing gas, as referred to in this invention, can be pure hydrogen or a hydrogen-containing gas; it is a gas stream containing an amount of hydrogen sufficient to carry out the intended reaction, and may contain one or more other gases (e.g., nitrogen and light hydrocarbons such as methane). The processing gas stream introduced into the reaction stage can contain at least about 50% by volume, for example, at least about 75% by volume, hydrogen. In some embodiments, the hydrogen processing gas can be substantially free of (less than 1% by volume) impurities such as H₂S and NH₃, and / or such impurities can be substantially removed from the processing gas before use.

[0070] Hydrogen can be produced at a rate of approximately 100 SCF / B (standard cubic feet of hydrogen per barrel of feed) (17 Nm³). 3 / m 3 ) to approximately 10000 SCF / B (1700 Nm 3 / m 3 The hydrogen is supplied at a rate of approximately 200 SCF / B (34 Nm³). 3 / m 3 ) to approximately 2500 SCF / B (420 Nm 3 / m 3 Hydrogen can be supplied to the hydrotreatment reactor and / or reaction zone in parallel with the input feed, or supplied separately to the hydrotreatment zone via a separate gas conduit.

[0071] Hydrotreating conditions can include: temperatures of 200°C to 450°C or 315°C to 425°C; pressures of 250 psig (1.8 MPag) to 5000 psig (34.6 MPag) or 300 psig (2.1 MPag) to 3000 psig (20.8 MPag); and a 0.1 hr time. -1 up to 10 hours -1 The liquid hourly space velocity (LHSV); and 200 scf / B (35.6 m 3 / m 3 Up to 10,000 SCF / B (1781m) 3 / m 3 ) or 500 (89m 3 / m 3 Up to 10,000 scf / B (1781m) 3 / m 3 The hydrogen processing rate.

[0072] In all respects, deasphalted oil can contact a hydrocracking catalyst under effective hydrocracking conditions. Hydrocracking catalysts typically comprise a base metal sulfide on an acidic support, such as amorphous silica-alumina, cracked zeolite like USY, or acidified alumina. These acidic supports are often mixed or combined with other metal oxides such as alumina, titanium dioxide, or silica. Examples of suitable acidic supports include acidic molecular sieves such as zeolites or aluminosilicates. One example of a suitable zeolite is USY, for example, USY zeolite with a unit size of 24.30 Å or less. Alternatively or concurrently, the catalyst can be a low-acidity molecular sieve, such as USY zeolite with a Si to Al ratio of at least about 20, for example, at least about 40 or 50. ZSM-48, for example, ZSM-48 with a SiO2 to Al2O3 ratio of about 110 or less, for example, about 90 or less, is another example of a suitable hydrocracking catalyst. Yet another option is to use a combination of USY and ZSM-48. Other options include the use of one or more of zeolite β, ZSM-5, ZSM-35, or ZSM-23, alone or in combination with the USY catalyst. Non-limiting examples of metals for hydrocracking catalysts include metals or combinations of metals containing at least one Group VIII metal, such as nickel, nickel-cobalt-molybdenum, cobalt-molybdenum, nickel-tungsten, nickel-molybdenum, and / or nickel-molybdenum-tungsten. Alternatively or alternatively, hydrocracking catalysts containing noble metals can also be used. Non-limiting examples of noble metal catalysts include catalysts based on platinum and / or palladium. Support materials that can be used for both noble and non-noble metal catalysts can comprise refractory oxide materials such as alumina, silica, alumina-silica, diatomaceous earth, magnesium oxide, zirconium oxide, or combinations thereof, with alumina, silica, and alumina-silica being the most common.

[0073] When only one hydrogenation metal is present on the hydrocracking catalyst, the amount of the hydrogenation metal, based on the total weight of the catalyst, can be at least about 0.1 wt%, for example, at least about 0.5 wt% or at least about 0.6 wt%. Alternatively or alternatively, when only one hydrogenation metal is present, the amount of the hydrogenation metal, based on the total weight of the catalyst, can be about 5.0 wt% or less, for example, about 3.5 wt% or less, about 2.5 wt% or less, about 1.5 wt% or less, about 1.0 wt% or less, about 0.9 wt% or less, about 0.75 wt% or less, or about 0.6 wt% or less. Also alternatively or alternatively, when more than one hydrogenation metal is present, the total amount of the hydrogenation metal, based on the total weight of the catalyst, can be at least about 0.1 wt%, for example, at least about 0.25 wt%, at least about 0.5 wt%, at least about 0.6 wt%, at least about 0.75 wt%, or at least about 1 wt%. Furthermore, or alternatively, when more than one hydrogenation metal is present, the total amount of the hydrogenation metal can be about 35% by weight or less, for example, about 30% by weight or less, about 25% by weight or less, about 20% by weight or less, about 15% by weight or less, about 10% by weight or less, or about 5% by weight or less, based on the total weight of the catalyst. In embodiments where the supported metal comprises a noble metal, the amount of the noble metal is typically less than about 2% by weight, for example, less than about 1% by weight, about 0.9% by weight or less, about 0.75% by weight or less, or about 0.6% by weight or less. It should be noted that hydrocracking under acidic conditions typically uses base metals (or multiple base metals) as the hydrogenation metal.

[0074] In various aspects, the hydrocracking conditions selected for the manufacture of lubricant base oils can depend on the desired conversion level, the contaminant content in the feedstock of the hydrocracking stage, and other feasible factors. For example, hydrocracking conditions in the first and / or second stages of a single-stage or multi-stage system can be selected to achieve the desired conversion level in the reaction system. Hydrocracking conditions can be referred to as acidic conditions or low-sulfur conditions, depending on the levels of sulfur and / or nitrogen present in the feedstock. For example, a feedstock with 100 wppm or less sulfur and 50 wppm or less nitrogen, such as less than 25 wppm sulfur and / or less than 10 wppm nitrogen, represents a feedstock for hydrocracking under low-sulfur conditions. In various aspects, thermally cracked residue oil, such as deasphalted oil derived from thermally cracked residue oil, can be hydrocracking. In some aspects, such as the use of an optional hydrotreating step prior to hydrocracking, thermally cracked residue oil can correspond to a low-sulfur feedstock. In other aspects, thermally cracked residue oil can represent a feedstock for hydrocracking under acidic conditions.

[0075] Hydrocracking under acidic conditions can be carried out at temperatures from about 550℉ (288℃) to about 840℉ (449℃), hydrogen partial pressures from about 1500psig to about 5000psig (10.3MPag to 34.6MPag), and for 0.05h. -1 Up to 10h -1 The liquid hourly space velocity and 35.6 m 3 / m 3 up to 1781m 3 / m 3 The process is carried out at a hydrogen processing gas rate of (200 SCF / B to 10,000 SCF / B). In other embodiments, the conditions can include a temperature ranging from about 600℉ (343°C) to about 815℉ (435°C), a hydrogen partial pressure of about 1500 psig to about 3000 psig (10.3 MPag to 20.9 MPag), and about 213 m 3 / m 3 Approximately 1068m 3 / m 3 Hydrogen processing gas rates ranging from 1200 SCF / B to 6000 SCF / B. The LHSV can reach approximately 0.25 h⁻¹. -1 approximately 50 hours -1 or about 0.5h -1 approximately 20 hours -1 For example, about 1.0h -1 From approximately 4.0h -1 .

[0076] In some respects, a portion of the hydrocracking catalyst can be incorporated into the second reactor stage. In this respect, the first reaction stage of the hydrotreating reaction system can contain one or more hydrotreating and / or hydrocracking catalysts. Conditions in the first reaction stage can be adapted to reduce the sulfur and / or nitrogen content of the feed. A separator can then be used between the first and second stages of the reaction system to remove gaseous sulfur and nitrogen contaminants. One option for the separator is simply gas-liquid separation to remove contaminants. Another option is to use a separator capable of separation at higher temperatures, such as a flash separator. This high-temperature separator can be used, for example, to separate the feed into portions with boiling points below the temperature fractionation point, such as about 350℉ (177°C) or about 400℉ (204°C), and portions with boiling points above the temperature fractionation point. In this type of separation, the naphtha boiling range portion of the effluent from the first reaction stage can also be removed, thereby reducing the volume of effluent processed in the second or other subsequent stages. Of course, any low-boiling-point contaminants from the effluent from the first stage will also be separated into the portion with boiling points below the temperature fractionation point. If sufficient pollutant removal is achieved in the first stage, the second stage can operate as a "low-sulfur" or low-pollutant stage.

[0077] Another option is to use a separator between the first and second stages of a hydrotreating reaction system, which is also capable of at least partially fractionating the effluent from the first stage. In this type of aspect, the effluent from the first hydrotreating stage can be separated into portions with boiling points at least below the distillate (e.g., diesel) fuel range, portions with boiling points within the distillate fuel range, and portions with boiling points above the distillate fuel range. The distillate fuel range can be defined based on the conventional diesel boiling range, such as a lower fractionation temperature having at least about 350℉ (177°C) or at least about 400℉ (204°C) to an upper fractionation temperature having about 700℉ (371°C) or less or 650℉ (343°C) or less. In some embodiments, for example by selecting a lower fractionation temperature of at least about 300℉ (149°C), the distillate fuel range can be extended to include additional kerosene.

[0078] In the case where interstage separators are also used to produce distillate fuel fractions, the portions with boiling points below the distillate fuel range include naphtha boiling range molecules, light fractions, and contaminants such as H2S. These different products can be separated from each other in any convenient manner. Similarly, one or more distillate fuel fractions can be formed from the distillate boiling range fractions if desired. The portions with boiling points above the distillate fuel range represent potential lubricant base oils. In these respects, the portions with boiling points above the distillate fuel range undergo further hydrogenation in the second hydrogenation stage.

[0079] Hydrocracking processes under low-sulfur conditions can be carried out under conditions similar to those used for sour hydrocracking processes, or the conditions can be different. In one embodiment, the conditions for the low-sulfur hydrocracking stage can be milder than those for the sour stage hydrocracking process. Hydrocracking conditions suitable for the non-sour stage can include, but are not limited to, conditions similar to those of the first stage or the sour stage. Suitable hydrocracking conditions can include temperatures from about 500℉ (260°C) to about 840℉ (449°C), hydrogen partial pressures from about 1500 psig to about 5000 psig (10.3 MPa to 34.6 MPa), and a 0.05 h⁻¹ of hydrogen. -1 Up to 10h -1 The liquid hourly space velocity and 35.6 m 3 / m 3 up to 1781m 3 / m 3 A hydrogen processing gas rate of (200 SCF / B to 10,000 SCF / B) is used. In other embodiments, the conditions can include a temperature ranging from about 600℉ (343°C) to about 815℉ (435°C), a hydrogen partial pressure of about 1500 psig to about 3000 psig (10.3 MPag to 20.9 MPag), and a hydrogen concentration of about 213 m³ / h.3 / m 3 Approximately 1068m 3 / m 3 Hydrogen processing gas rates ranging from 1200 SCF / B to 6000 SCF / B. The LHSV can reach approximately 0.25 h⁻¹. -1 approximately 50 hours -1 or about 0.5h -1 approximately 20 hours -1 For example, about 1.0h -1 From approximately 4.0h -1 .

[0080] In another aspect, the same conditions can be used for both hydrotreatment and hydrocracking beds or stages, for example, both using hydrotreatment conditions or both using hydrocracking conditions. In yet another embodiment, the pressures of the hydrotreatment and hydrocracking beds or stages can be the same.

[0081] In another aspect, the hydrocracking reaction system can include more than one hydrocracking stage. If multiple hydrocracking stages exist, at least one hydrocracking stage can have the effective hydrocracking conditions described above, including a hydrogen partial pressure of at least about 1500 psig (10.3 MPa). In this respect, other hydrocracking processes can be carried out under conditions that may include lower hydrogen partial pressures. Suitable hydrocracking conditions for additional hydrocracking stages can include, but are not limited to, a temperature of about 500℉ (260°C) to about 840℉ (449°C), a hydrogen partial pressure of about 250 psig to about 5000 psig (1.8 MPa to 34.6 MPa), and a 0.05 h⁻¹. -1 Up to 10h -1 The liquid hourly space velocity and 35.6 m 3 / m 3 up to 1781m 3 / m 3 Hydrogen processing gas rates of 200 SCF / B to 10,000 SCF / B. In other embodiments, conditions for the additional hydrocracking stage can include temperatures ranging from about 600℉ (343°C) to about 815℉ (435°C), hydrogen partial pressures of about 500 psig to about 3000 psig (3.5 MPag to 20.9 MPa), and a hydrogen concentration of about 213 m³ / h. 3 / m 3 Approximately 1068m 3 / m 3 Hydrogen processing gas rates ranging from 1200 SCF / B to 6000 SCF / B. The LHSV can reach approximately 0.25 h⁻¹. -1 approximately 50 hours -1 or about 0.5h -1 approximately 20 hours -1For example, about 1.0h -1 From approximately 4.0h -1 .

[0082] Additional hydrogenation operations—catalytic dewaxing, hydrorefining, and optional hydrocracking.

[0083] In some alternative aspects, at least the lubricant boiling range portion of the hydrotreated deasphalted oil can be contacted with additional hydrotreating operations (including catalytic dewaxing) to form Group I and / or Group II base oils, including Group I and / or Group II bright oils. In some aspects, the first lubricant boiling range portion of the hydrotreated deasphalted oil can be solvent dewaxed as described above, while the second lubricant boiling range portion can be contacted with additional hydrotreating operations. In other aspects, solvent dewaxing alone or additional hydrotreating alone can be used to treat the lubricant boiling range portion of the hydrotreated deasphalted oil.

[0084] In some embodiments, additional hydrotreating of the lubricant boiling range portion of the hydrotreated deasphalted oil can also be included before and / or after contact with hydrocracking conditions. At this point in the process, hydrocracking can be considered “low-sulfur” hydrocracking because the sulfur content of the hydrotreated deasphalted oil can be 200 wppm or less.

[0085] Suitable hydrocracking conditions can include contacting the feedstock with the hydrocracking catalyst as described above. In some embodiments, USY zeolite with a silica-to-alumina ratio of at least 30 and a unit cell size of less than 24.32 angstroms is preferably used as the zeolite for the hydrocracking catalyst, thereby improving the VI uptake of hydrocracking and / or improving the ratio of distillate fuel yield to naphtha fuel yield in the fuel boiling range products.

[0086] Suitable hydrocracking conditions can also include temperatures from about 500℉ (260℃) to about 840℉ (449℃), hydrogen partial pressures from about 1500psig to about 5000psig (10.3MPag to 34.6MPag), and a 0.05h... -1 Up to 10h -1 The liquid hourly space velocity and 35.6 m 3 / m 3 up to 1781m 3 / m 3 A hydrogen processing gas rate of (200 SCF / B to 10,000 SCF / B) is used. In other embodiments, the conditions can include a temperature ranging from about 600℉ (343°C) to about 815℉ (435°C), a hydrogen partial pressure of about 1500 psig to about 3000 psig (10.3 MPa g to 20.9 MPa), and a hydrogen concentration of about 213 m³ / h. 3 / m 3 Approximately 1068m 3 / m3 Hydrogen processing gas rates ranging from 1200 SCF / B to 6000 SCF / B. The LHSV can reach approximately 0.25 h⁻¹. -1 approximately 50 hours -1 or about 0.5h -1 approximately 20 hours -1 For example, about 1.0h -1 From approximately 4.0h -1 .

[0087] For catalytic dewaxing, suitable dewaxing catalysts can contain molecular sieves, such as crystalline aluminosilicates (zeolites). In one embodiment, the molecular sieve can contain, or consist essentially of, ZSM-22, ZSM-23, ZSM-48, or be ZSM-22, ZSM-23, ZSM-48. In some embodiments, molecular sieves selected for dewaxing (rather than cracking) by isomerization can be used, such as ZSM-48, ZSM-23, or combinations thereof. Alternatively or additionally, the molecular sieve can contain, or consist essentially of, 10-membered ring 1-D molecular sieves, or be 10-membered ring 1-D molecular sieves, such as EU-2, EU-11, ZBM-30, ZSM-48, or ZSM-23. For example, ZSM-48 is used. Note that zeolites having a ZSM-23 structure and a silica to alumina ratio of about 20:1 to about 40:1 can sometimes be referred to as SSZ-32. In some embodiments, the dewaxing catalyst may contain a binder for molecular sieves such as alumina, titanium dioxide, silica, silica-alumina, zirconium oxide, or combinations thereof, for example, alumina and / or titanium dioxide or silica and / or zirconium oxide and / or titanium dioxide.

[0088] In some embodiments, the dewaxing catalyst used in the method according to the invention is a catalyst having a low silica to alumina ratio. For example, for ZSM-48, the silica to alumina ratio in the zeolite can be about 100:1 or less, such as about 90:1 or less, or about 75:1 or less, or about 70:1 or less. Alternatively or alternatively, the silica to alumina ratio in ZSM-48 can be at least about 50:1, such as at least about 60:1 or at least about 65:1.

[0089] In various embodiments, the catalyst according to the invention further comprises a metal hydrogenation component. The metal hydrogenation component is typically a Group VI and / or Group VIII metal. In some embodiments, the metal hydrogenation component can be a combination of a non-noble Group VIII metal and a Group VI metal. Suitable combinations can include Ni, Co, or Fe with Mo or W, for example, Ni with Mo or W.

[0090] Metal hydrogenation components can be added to the catalyst in any convenient manner. One technique for adding metal hydrogenation components is the initial wet process. For example, after combining zeolite and binder, the combined zeolite and binder can be extruded into catalyst particles. These catalyst particles can then be contacted with a solution containing a suitable metal precursor. Alternatively, the metal can be added to the catalyst via ion exchange, wherein the metal precursor is added to the mixture of zeolite (or zeolite and binder) prior to extrusion.

[0091] Based on the catalyst, the amount of metal in the catalyst can be at least 0.1 wt%, at least 0.5 wt%, at least 1.0 wt%, at least 2.5 wt%, or at least 5.0 wt%. Based on the catalyst, the amount of metal in the catalyst can be 20 wt% or less, 10 wt% or less, 5 wt% or less, 2.5 wt% or less, or 1 wt% or less. For embodiments where the metal is a combination of non-noble Group VIII and Group VI metals, the total amount of metal can be from 0.5 wt% to 20 wt%, from 1 wt% to 15 wt%, or from 2.5 wt% to 10 wt%.

[0092] The dewaxing catalyst that can be used in the method according to the invention can also contain a binder. In some embodiments, the dewaxing catalyst used in the method according to the invention is formulated using a low surface area binder, wherein the low surface area binder represents a surface area of ​​100 m². 2 / g or less or 80m 2 / g or less or 70m 2 / g or less of adhesive. Alternatively or alternatively, the adhesive can have at least about 25m 2 / g surface area. The amount of zeolite in the catalyst formulated with a binder can be from about 30% by weight to 90% by weight of zeolite relative to the total weight of the binder and zeolite. In some embodiments, the amount of zeolite is at least about 50% by weight of the total weight of the zeolite and binder, for example at least about 60% by weight or about 65% by weight to about 80% by weight.

[0093] Unbound by any particular theory, it is believed that the use of low-surface-area binders reduces the amount of binder surface area available for the hydrogenation metal supported on the catalyst. This results in an increase in the amount of hydrogenation metal supported within the molecular sieve pores of the catalyst.

[0094] Zeolites can be incorporated with binders in any convenient manner. For example, a bound catalyst can be manufactured by starting with powders of both zeolite and binder, combining the powders with added water and grinding to form a mixture, and then extruding the mixture to produce a catalyst of desired size. Extrusion aids can also be used to modify the extrusion flow properties of the zeolite and binder mixture. The amount of framework alumina in the catalyst can range from 0.1 to 3.33 wt%, or 0.1 to 2.7 wt%, or 0.2 to 2 wt%, or 0.3 to 1 wt%.

[0095] Effective conditions for catalytic dewaxing of the feed in the presence of a dewaxing catalyst can include: temperatures of 280°C to 450°C, for example, 343°C to 435°C; hydrogen partial pressures of 3.5 MPag to 34.6 MPag (500 psig to 5000 psig), for example, 4.8 MPag to 20.8 MPag; and 178 m 3 / m 3 (1000SCF / B) to 1781m 3 / m 3 (10,000 SCF / B), for example, 213m 3 / m 3 (1200SCF / B) to 1068m 3 / m 3 The hydrogen circulation rate is 6000 SCF / B. The LHSV can reach approximately 0.2 h. -1 approximately 10 hours -1 For example, about 0.5h -1 approximately 5 hours -1 and / or about 1 hour -1 approximately 4 hours -1 .

[0096] Before and / or after catalytic dewaxing, the deasphalted oil from the hydrotreating operation (i.e., at least its lubricant boiling range portion) can be contacted with an aromatic saturated catalyst, which can be alternatively referred to as a hydrorefining catalyst. Contact with the aromatic saturated catalyst can occur before or after fractionation. If aromatic saturation occurs after fractionation, one or more fractions of the fractionated product can be aromaticly saturated. Alternatively, all effluent from the final hydrocracking or dewaxing process can be hydrorefined and / or aromatically saturated.

[0097] Hydrorefining and / or aromatic compound saturation catalysts can comprise catalysts containing Group VI metals, Group VIII metals, and mixtures thereof. In one embodiment, the metal comprises at least one metal sulfide with strong hydrogenation function. In another embodiment, the hydrorefining catalyst can comprise a Group VIII noble metal such as Pt, Pd, or combinations thereof. Mixtures of metals can also be present as bulk metal catalysts, wherein the amount of metal is about 30% by weight or more based on the catalyst. For supported hydrorefining catalysts, suitable metal oxide supports comprise low-acid oxides such as silica, alumina, silica-alumina, or titanium dioxide, such as alumina. Exemplary hydrorefining catalysts for aromatic compound saturation will comprise at least one metal with relatively strong hydrogenation function on a porous support. Typical support materials include amorphous or crystalline oxide materials such as alumina, silica, and silica-alumina. Support materials can also be modified, for example, by halogenation or, in particular, fluorination. For non-noble metals, the metal content of the catalyst is typically up to about 20% by weight. In one embodiment, the hydrorefining catalyst may comprise a crystalline material belonging to the M41S class or series of catalysts. The M41S series of catalysts are mesoporous materials with a high silica content. Examples include MCM-41, MCM-48, and MCM-50. An exemplary member of this class is MCM-41.

[0098] Hydrorefining conditions can include: temperatures from about 125°C to about 425°C, for example from about 180°C to about 280°C; hydrogen partial pressures from about 500 psig (3.4 MPa) to about 3000 psig (20.7 MPa), for example from about 1500 psig (10.3 MPa) to about 2500 psig (17.2 MPa); and about 0.1 hr -1 approximately 5 hours -1 LHSV, for example, about 0.5hr -1 From approximately 1.5 hours -1 The liquid hourly space velocity. Additionally, it is possible to use 35.6 m / s. 3 / m 3 up to 1781m 3 / m 3 Hydrogen processing gas rates ranging from 200 SCF / B to 10,000 SCF / B.

[0099] Solvent treatment of catalytic dewaxing effluent or catalytic dewaxing input stream

[0100] For deasphalted oils derived from propane deasphalting, further hydrotreating (including catalytic dewaxing) can be sufficient to produce lubricant base oils with low haze formation and unexpected compositional properties. For oils derived from C... 4+Deasphalted oil, after further hydrotreating operations (including catalytic dewaxing), can undergo solvent treatment of the resulting catalytic dewaxing effluent to form one or more lubricant base oil products with a tendency to reduce or eliminate haze formation. The type of solvent treatment can depend on the nature of the initial hydrotreating operation (hydrotreating and / or hydrocracking) and the nature of the subsequent hydrotreating operation (including dewaxing).

[0101] In aspects where the initial hydrotreating operation is less demanding, corresponding to a conversion rate of 10% to 40% by weight relative to about 700℉ (370°C), the subsequent solvent treatment can correspond to solvent dewaxing. Solvent dewaxing can be carried out in a manner similar to that described above. However, this solvent dewaxing can be used to manufacture Group II lubricant base oils. In some aspects, when the initial hydrotreating operation corresponds to a conversion rate of 10% to 40% by weight relative to 370°C, catalytic dewaxing during additional hydrotreating operations can also be carried out at a lower degree of demand, such that at least 6% or at least 8% or at least 10% or at least 12% or at least 15% by weight, for example up to 20% by weight, of wax is retained in the catalytic dewaxing effluent. The wax content in the catalytic dewaxing effluent can then be reduced by 2% to 10% by weight using solvent dewaxing. This enables the production of solvent-dewaxed oil products with a wax content of 0.1% to 12% by weight, or 0.1% to 10% by weight, or 0.1% to 8% by weight, or 0.1% to 6% by weight, or 1% to 12% by weight, or 1% to 10% by weight, or 1% to 8% by weight, or 4% to 12% by weight, or 4% to 10% by weight, or 4% to 8% by weight, or 6% to 12% by weight, or 6% to 10% by weight. Specifically, the solvent-dewaxed oil can have a wax content of 0.1% to 12% by weight, or 0.1% to 6% by weight, or 1% to 10% by weight, or 4% to 12% by weight.

[0102] In various aspects, subsequent solvent treatment can correspond to solvent extraction. Solvent extraction can be used to reduce the content of aromatic compounds and / or the amount of polar molecules. The solvent extraction process selectively dissolves aromatic compound components to form an aromatic-rich extract phase, while leaving more paraffin components in the aromatic-poor raffinate phase. Cycloalkanes are distributed between the extract phase and the raffinate phase. Typical solvents for solvent extraction include phenol, furfural, and N-methylpyrrolidone. The degree of separation between the extract phase and the raffinate phase can be controlled by controlling the solvent-to-oil ratio, the extraction temperature, and the contact between the distillate to be extracted and the solvent. Any convenient type of liquid-liquid extractor, such as a countercurrent liquid-liquid extractor, can be used. Depending on the initial concentration of aromatic compounds in the deasphalted oil, the raffinate phase can have an aromatic compound content of 5% to 25% by weight and / or a saturated compound content of 75% to 95% by weight (or greater). For a typical feed, the aromatic compound content can be at least 10% by weight and / or the saturated compound content can be 90% by weight or less. In all respects, the raffinate yield from solvent extraction can be at least 40% by weight, at least 50% by weight, at least 60% by weight, or at least 70% by weight.

[0103] In some embodiments, the raffinate from solvent extraction can be incompletely extracted. In these aspects, extraction is carried out in a manner that maximizes the raffinate yield while still removing most of the lowest quality molecules from the feed. The raffinate yield can be maximized by controlling the extraction conditions, for example by reducing the solvent-to-oil ratio and / or lowering the extraction temperature.

[0104] Solvent-treated oils (solvent-dewaxed or solvent-extracted) can have pour points of -6°C or less, -10°C or less, -15°C or less, or -20°C or less, depending on the nature of the target lubricant base oil product. Alternatively or concurrently, solvent-treated oils (solvent-dewaxed or solvent-extracted) can have cloud points of -2°C or less, -5°C or less, or -10°C or less, depending on the nature of the target lubricant base oil product. Pour points and cloud points can be determined according to ASTM D97 and ASTM D2500, respectively. The resulting solvent-treated oils are suitable for forming one or more types of Group II base oils. The resulting solvent-dewaxed oils can have a viscosity index of at least 80, at least 90, at least 95, at least 100, at least 110, or at least 120. The viscosity index can be determined according to ASTM D2270. In some embodiments, at least 10% by weight (or at least 20% by weight or at least 30% by weight) of the resulting solvent-treated oil corresponds to a Group II bright oil with a kinematic viscosity of at least 14 cSt, at least 15 cSt, at least 20 cSt, at least 25 cSt, at least 30 cSt, or at least 32 cSt at 100°C, for example, up to 50 cSt or greater. Alternatively or alternatively, the Group II bright oil may have a kinematic viscosity of at least 300 cSt, at least 320 cSt, at least 340 cSt, or at least 350 cSt at 40°C, for example, up to 500 cSt or greater. The kinematic viscosity can be determined according to ASTM D445. Alternatively or alternatively, the Concordant carbon content may be about 0.1% by weight or less, or about 0.02% by weight or less. The Concordant carbon content can be determined according to ASTM D4530. Alternatively or concurrently, the resulting base oil may have a turbidity of at least 1.5 (in combination with a cloud point below 0°C), or a turbidity of at least 2.0 and / or a turbidity of 4.0 or less, 3.5 or less, or 3.0 or less. In particular, the turbidity may be 1.5 to 4.0, 1.5 to 3.0, 2.0 to 4.0, or 2.0 to 3.5.

[0105] By reducing or minimizing the difference between the cloud point and pour point temperatures of the lubricant base oil, it can be demonstrated that the tendency of lubricant base oils formed from solvent-treated oils to form haze is reduced or eliminated. In all aspects, the difference between the cloud point and pour point of the resulting solvent-dewaxed oil and / or one or more Group II lubricant base oils (including one or more bright oils formed from solvent-treated oils) can be 22°C or less, or 20°C or less, or 15°C or less, or 10°C or less, for example, as low as about 1°C.

[0106] In some alternatives, the solvent treatment described above can be carried out prior to catalytic dewaxing.

[0107] Group II base oilseed products

[0108] For deasphalted oils derived from propane, butane, pentane, hexane, and higher alkanes or mixtures thereof, additional hydrotreating operations (including catalytic dewaxing) and potential solvent treatments can be sufficient to produce lubricant base oils with low (or no) haze formation and improved compositional properties. Currently manufactured conventional products with a kinematic viscosity of approximately 32 cSt at 100°C contain more than 10% by weight of aromatic compounds and / or more than 0.03% by weight of sulfur compared to the base oil.

[0109] In various aspects, the base oils produced according to the method of the present invention can have a kinematic viscosity of at least 14 cSt, at least 20 cSt, at least 25 cSt, at least 30 cSt, or at least 32 cSt at 100°C and can contain less than 10% by weight of aromatic compounds, more than 90% by weight of saturated compounds, and less than 0.03% by weight of sulfur. In some embodiments, the content of saturated compounds can be much higher, for example, more than 95% by weight or more than 97% by weight. Furthermore, detailed characterization of the "branching" (branching) of the molecules by C-NMR reveals a high degree of branching, which can be quantified by examining the absolute number of methyl branches, ethyl branches, or propyl branches, or combinations thereof, respectively. Branching can also be quantified by observing the ratio of branching points (methyl, ethyl, or propyl) to the number of internal carbons labeled as ε-carbons by C-NMR. Quantification of branching by ε-carbons can be used to determine whether the base oil will stabilize over time to prevent haze formation. For the purposes reported herein... 13 C-NMR results show that the sample can be prepared into a solution of 25 to 30 wt% acetylacetone chromium(III) in CDCl3 with 7% added as a relaxant. The analysis was performed on a JEOL ECS NMR spectrometer with a proton resonance frequency of 400 MHz. 13 ¹³C NMR experiments. Quantitative analysis was performed at 27°C using an inversely gated decoupling experiment with a 45° flip angle, 6.6 seconds between pulses, 64K data points, and 2400 scans. 13 C10 NMR experiments. Spectral reference was taken at 0 ppm using TMS. Spectra were processed with line broadening from 0.2 to 1 Hz and baseline correction was applied before manual integration. The entire spectrum was integrated to determine the mole percentage in different integration regions as follows: 170 to 190 PPM (aromatic C); 30 to 29.5 PPM (ε-carbon); 15 to 14.5 PPM (terminal and side-chain propyl groups); 14.5 to 14 PPM - terminal methyl (α-) of long chains; 12 to 10 PPM (side-chain and terminal ethyl groups). Total methyl content could be obtained by proton NMR. The methyl signal at 0 to 1.1 PPM could be integrated. The entire spectrum could be integrated to determine the mole percentage of methyl. The mole percentage of methyl could be converted to total methyl using the average carbon number obtained from gas chromatography.

[0110] It has also been found that, using Fourier transform ion cyclotron resonance-mass spectrometry (FTICR-MS) and / or field desorption mass spectrometry (FDMS), the prevalence of smaller cycloalkane ring structures with fewer than 6, 7, or 8 rings can be similar, but the remaining number of larger cycloalkane ring structures with 7 or more rings, or 8+ rings, 9+ rings, or 10+ rings is reduced in base oils that are stable against fog formation.

[0111] The FTICR-MS results reported herein were generated according to the method described in U.S. Patent No. 9,418,828. The method described in U.S. Patent No. 9,418,828 generally involves laser desorption / ionization of petroleum saturated molecules (including 538°C+ molecules) using laser-induced desorption / ionization with Ag ion complexation (LDI-Ag) without destroying the molecular ionic structure. Ultra-high resolution Fourier transform ion cyclotron resonance mass spectrometry was applied to determine the precise elemental formulas and corresponding abundances of the saturated compound-Ag cations. The saturated compound fraction compositions can be arranged by homologues and molecular weight. The portion of U.S. Patent No. 9,418,828 relating to the determination of the content of saturated ring structures in a sample is incorporated herein by reference.

[0112] For the FDMS results reported in this paper, field desorption (FD) is a soft ionization method in which a high-potential electric field is applied to an emitter (a filament that has formed tiny “whiskers”) coated with a diluted sample, causing the gaseous molecules of the analyte to ionize. The mass spectra produced by FD consist of molecular radicals and cations M + Or in some cases, protonated molecular ions [M] + H] + Dominance. Because FDMS cannot distinguish between molecules with "n" cycloalkane rings and molecules with "n+7" rings, FDMS data is "corrected" using FTICR-MS data derived from the most similar sample. FDMS correction is performed by applying the resolved "n" to "n+7" ring ratio from FTICR-MS to the unresolved FDMS data for that particular class of molecules.

[0113] Further research has revealed that base oils with the above-mentioned composition offer the advantage of being fog-free at the start of manufacturing and maintaining fog-free status over a long period. This is an advantage over prior art heavy base oils with highly saturated compounds.

[0114] Furthermore, it has been found that the base oils of the present invention can be blended with additives to form formulated lubricants, such as, but not limited to, marine oils, engine oils, greases, paper machine oils, and gear oils. These additives may include, but are not limited to, detergents, dispersants, antioxidants, viscosity modifiers, and pour point depressants. When blended in this way, performance measured by standard low-temperature tests such as miniature rotational viscometers (MRVs) and Brookfield tests has shown to be superior to formulations blended with conventional base oils.

[0115] It has also been found that when common additives, such as but not limited to defoamers, pour point depressants, antioxidants, and rust inhibitors, are blended into industrial oils, their oxidation performance is superior to that of conventional base oils in standard oxidation tests, such as the U.S. Steel Oxidation Test.

[0116] Other performance parameters, such as interfacial properties, sediment control, storage stability, and toxicity, have also been tested and are similar to or better than those of conventional base oils.

[0117] In addition to blending with additives, the base oils of this invention can be blended with other base oils to prepare base oils. These other base oils may include solvent-treated base oils, hydrotreated base oils, synthetic base oils, base oils derived from the Fisher-Tropsch process, PAO, and naphthenic base oils. Alternatively or alternatively, other base oils may include Group I, Group II, Group III, Group IV, and / or Group V base oils. Alternatively or alternatively, one or more low-viscosity base oils may be combined with the high-viscosity base oils of this invention to produce extreme bimodal blends. In some embodiments, the low-viscosity base oil may be any one or more of the following: light neutral base oils, medium neutral base oils, heavy neutral base oils, Group I base oils, Group II base oils, Group III base oils, Group IV base oils, Group V base oils, or any combination thereof. The kinematic viscosity of the low-viscosity base oil at 100°C can be as high as 2 cSt, 3 cSt, 4 cSt, 5 cSt, 6 cSt, 7 cSt, 8 cSt, 9 cSt, 10 cSt, 11 cSt, or 12 cSt. In some embodiments, the ratio of the amount of the low-viscosity base oil to the amount of the high-viscosity base oil of the present invention can be as high as 1:99, 5:95, 10:90, 20:80, 30:70, 40:60, 50:50, 60:40, 70:30, 80:20, 90:10, 95:5, or 99:1.

[0118] Alternatively or concurrently, other types of base oils used for blending may include hydrocarbon aromatic compounds, alkylated aromatic compounds, esters (including synthetic esters and / or renewable esters), and / or other unconventional or non-standardized base oils. These base oil blends of the base oils of the present invention and other base oils may also be combined with additives such as those mentioned herein to prepare formulated lubricants.

[0119] The fluid formulations of this invention may contain one or more performance additives, including but not limited to anti-wear additives, detergents, dispersants, viscosity modifiers, corrosion inhibitors, rust inhibitors, metal passivators, extreme pressure additives, anti-galling agents, wax modifiers, viscosity index improvers, filtration loss reducers, sealing compatibilizers, friction modifiers, lubricants, anti-staining agents, colorants, defoamers, demulsifiers, emulsifiers, thickeners, wetting agents, gelling agents, adhesives, colorants, etc. These additives are typically delivered with varying amounts of diluent oil, ranging from 5% by weight to 50% by weight.

[0120] The additives that can be used in the fluids of this invention need not be soluble in the fluid. Insoluble additives, such as zinc stearate in oil, can be dispersed as a suspension in the fluids of this invention.

[0121] Furthermore, it has been found that the base oil of the present invention can be used as a thickener in the formulation of fluids to obtain a desired viscosity. The base oil of the present invention can be used in combination with other thickeners. The base oil of the present invention can be used as a thickener in place of other thickeners. Using the base oil of the present invention as a thickener can reduce or eliminate the use of other thickeners. For example, the amount of another thickener in the formulation of the fluid can be reduced by up to 0.1%, up to 1%, up to 5%, up to 10%, up to 20%, up to 30%, up to 40%, up to 50%, up to 60%, up to 70%, up to 80%, up to 90%, up to 95%, or up to 100%.

[0122] Fluid formulations containing the base oils of this invention as thickeners can exhibit similar viscosity properties to equivalent fluid formulations containing one or more other thickeners but not the base oils of this invention. Compared to equivalent fluid formulations containing one or more other thickeners but not the base oils of this invention, fluid formulations containing the base oils of this invention as thickeners can exhibit enhanced properties (e.g., oxidation resistance, low-temperature flowability, and / or deposit control). Compared to equivalent fluid formulations containing one or more other thickeners but not the base oils of this invention, fluid formulations containing the base oils of this invention as thickeners can be blended at a lower cost.

[0123] Examples of other thickeners include viscosity index improvers and other high-viscosity base oils. An exemplary viscosity index improver is a polyisobutylene polymer, which can be used to thicken formulated fluids to obtain the desired lubricant viscosity. Polyisobutylene can be present in the formulated fluid at a treatment rate of 1% to 20% by weight. The use of polyisobutylene can be reduced or eliminated by using the base oils of this invention.

[0124] Furthermore, by using the base oils of the present invention, the use of other high-viscosity base oils in the formulated fluid can be reduced or eliminated. Exemplary high-viscosity base oils include Class I bright oils and high-viscosity PAO. By using the base oils of the present invention in the formulated fluid, the amount of another high-viscosity base oil in the formulated fluid can be reduced by up to 0.1%, up to 1%, up to 5%, up to 10%, up to 20%, up to 30%, up to 40%, up to 50%, up to 60%, up to 70%, up to 80%, up to 90%, up to 95%, or up to 100%.

[0125] In some fluid formulations, multiple PAO components may be present, and the base oil of the present invention can reduce or replace a single PAO component, while retaining other PAO components in the formulated fluid. In other embodiments, the base oil of the present invention can partially or completely replace multiple PAO components, and other PAO components are still retained in the formulated lubricant.

[0126] The type and amount of performance additives used in combination with the present invention in lubricant compositions are not limited to the examples shown herein.

[0127] Other additives - cleaning agents

[0128] Exemplary cleaning agents that can be used in this invention include, for example, alkali metal cleaning agents, alkaline earth metal cleaning agents, or mixtures of one or more alkali metal cleaning agents with one or more alkaline earth metal cleaning agents. Typical cleaning agents are anionic materials comprising a long-chain hydrophobic portion of the molecule and a smaller anionic or oleophobic hydrophilic portion of the molecule. The anionic portion of the cleaning agent is typically derived from organic acids such as sulfuric acid, carboxylic acid, phosphorous acid, phenol, or mixtures thereof. The ion is typically an alkaline earth metal or alkali metal.

[0129] Salts containing substantially stoichiometric amounts of metal are described as neutral salts and have a total base number (TBN, measured according to ASTM D2896) from 0 to 80. Many compositions are superalkaline, containing a large amount of metal, obtained by reacting an excess of a metal compound (e.g., metal hydroxide or oxide) with an acidic gas (e.g., carbon dioxide). Available cleaners can be neutral, slightly superalkaline, or highly superalkaline. These cleaners can be used in mixtures of neutral, superalkaline, and highly superalkaline calcium salicylate, sulfonates, phenolates, and / or magnesium salicylate, sulfonates, and phenolates. The TBN range can vary from low to high TBN products, including from as low as 0 to as high as 600. Mixtures of low, medium, and high TBN, as well as mixtures of calcium and magnesium metal cleaners, can be used, including sulfonates, phenolates, salicylates, and carboxylates. Cleaner mixtures with a metal-to-cleaner ratio of 1, 2, and up to 5 can be used. Boronized cleaners can also be used.

[0130] Alkaline earth metal phenolates are another class of useful cleaning agents. These agents can be prepared by reacting alkaline earth metal hydroxides or oxides (e.g., CaO, Ca(OH)₂, BaO, Ba(OH)₂, MgO, Mg(OH)₂) with alkylphenols or sulfide alkylphenols. Useful alkyl groups include straight-chain or branched C1-C groups. 30 Alkyl groups, such as C4-C 20 Or mixtures thereof. Examples of suitable phenols include isobutylphenol, 2-ethylhexylphenol, nonylphenol, dodecylphenol, etc. It should be noted that the starting alkylphenol may contain more than one independently linear or branched alkyl substituent and can be used in amounts from 0.5 to 6% by weight. When using unsulfurized alkylphenols, the sulfided product can be obtained by methods well known in the art. These methods involve: heating a mixture of alkylphenol and a sulfiding agent (including elemental sulfur, sulfur halides such as sulfur dichloride, etc.); and then reacting the sulfided phenol with an alkaline earth metal alkali.

[0131] Metal salts of carboxylic acids can also be used as cleaning agents. These carboxylic acid cleaning agents can be prepared by reacting an alkaline metal compound with at least one carboxylic acid and removing free water from the reaction products. These compounds can be hyperalkaline to produce the desired TBN level. Cleaning agents made from salicylic acid are an exemplary class of cleaning agents derived from carboxylic acids. Useful salicylates include long-chain alkyl salicylates. A useful series of compositions has the following formula:

[0132]

[0133] Where R is an alkyl group having 1 to 30 carbon atoms, n is an integer from 1 to 4, and M is an alkaline earth metal. Example: The R group contains at least C... 11 For example, C13 Or a larger alkyl chain. R can be substituted with substituents that do not affect the cleaning agent's function. M can be calcium, magnesium, or barium. In some embodiments, M is calcium.

[0134] Hydroxyl-substituted salicylic acids can be prepared from phenol via the Kolbe reaction (see U.S. Patent 3,595,791). Metal salts of alkyl-substituted salicylic acids can be prepared by metathesis of the metal salt in a polar solvent such as water or alcohol.

[0135] Alkaline earth metal phosphates are also used as cleaning agents and are known in the art.

[0136] The cleaning agent can be a simple cleaning agent or a so-called blended or compound cleaning agent. The latter type of cleaning agent can provide the properties of two cleaning agents without needing to blend the separate materials. See U.S. Patent No. 6,034,039.

[0137] Examples of cleaning agents may include calcium phenolate, calcium sulfonate, calcium salicylate, magnesium phenolate, magnesium sulfonate, magnesium salicylate, and other related components (including boronized cleaning agents) and mixtures thereof. Example mixtures of cleaning agents may include magnesium sulfonate and calcium salicylate, magnesium sulfonate and calcium sulfonate, magnesium sulfonate and calcium phenolate, calcium phenolate and calcium salicylate, calcium phenolate and calcium sulfonate, calcium phenolate and magnesium salicylate, and calcium phenolate and magnesium phenolate.

[0138] Another category of detergents is oil-soluble, ashless nonionic detergents. Typical nonionic detergents are polyoxyethylene, polyoxypropylene, polyoxybutylene alkyl ethers, or nonylphenol ethoxylates. For reference, see "Nonionic Surfactants: Physical Chemistry," Martin J. Schick, CRC Press; 2nd edition (March 27, 1987). These detergents are less common in engine lubricant formulations but offer several advantages, such as improved solubility in ester-based oils. Hydrocarbon-soluble nonionic detergents typically have a hydrophilic-lipophilic balance (HLB) value of 10 or less.

[0139] To minimize the impact of ash deposits on engine knock and pre-ignition (including low-speed pre-ignition), the cleaning agent should be an ashless nonionic cleaner with a hydrophilic-lipophilic balance (HLB) value of 10 or less. These cleaners are commercially available from: for example, Croda Inc., under the trade names “Alarmol PS11E” and “Alarmol PS15E”; and Dow Chemical Co., under the trade names “Ecosurf EH-3”, “Tergitol 15-S-3”, “Tergitol L-61”, “Tergitol L-62”, “Tergitol NP-4”, “Tergitol NP-6”, “Tergitol NP-7”, “Tergitol NP-8”, “Tergitol NP-9”, “Triton X-15”, and “Triton X-35”.

[0140] Based on the total weight of the lubricating oil, the concentration of detergent in the lubricating oil of the present invention can range from 0.5 to 6.0 wt%, for example, 0.6 to 5.0 wt% or 0.8 wt% to 4.0 wt%.

[0141] Other additives - dispersants

[0142] During engine operation, insoluble oxidation byproducts are generated. Dispersants help retain these byproducts in solution, thereby reducing their deposition on metal surfaces. Dispersants used in lubricant formulations can be ashless or ash-forming in nature. In some embodiments, the dispersant is ashless. A so-called ashless dispersant is an organic material that does not substantially form ash upon combustion. For example, dispersants containing nonmetals or non-borate metals are considered ashless. Conversely, the metal-containing detergents discussed above form ash upon combustion.

[0143] Suitable dispersants typically contain polar groups attached to relatively high molecular weight hydrocarbon chains. These polar groups usually contain at least one element from nitrogen, oxygen, or phosphorus. A typical hydrocarbon chain contains 50 to 400 carbon atoms.

[0144] One particularly useful class of dispersants is alkenyl succinic acid derivatives, typically prepared by reacting long-chain hydrocarbon-substituted succinic acid compounds (usually hydrocarbon-substituted succinic anhydrides) with polyhydroxy or polyamino compounds. The long-chain hydrocarbon groups constituting the lipophilic portion of the molecule that imparts solubility in oil are typically polyisobutylene groups.

[0145] Hydrocarbon-substituted succinic acids and hydrocarbon-substituted succinic anhydride derivatives are useful dispersants. In particular, succinimides, succinates, or succinate amides prepared by reacting, for example, a hydrocarbon-substituted succinic acid compound having at least 50 carbon atoms in the hydrocarbon substituent with at least one equivalent of an alkylimide are especially useful, although sometimes hydrocarbon substituents having 20 to 50 carbon atoms can be useful.

[0146] Succinimide is formed via a condensation reaction between a hydrocarbon-substituted succinic anhydride and an amine. The molar ratio can vary depending on the polyamine. For example, the molar ratio of hydrocarbon-substituted succinic anhydride to TEPA can vary from 1:1 to 5:1.

[0147] Succinates are formed by the condensation reaction between hydrocarbon-substituted succinic anhydrides and alcohols or polyols. The molar ratio can vary depending on the alcohol or polyol used. For example, the condensation product of hydrocarbon-substituted succinic anhydrides and pentaerythritol is a useful dispersant.

[0148] Succinate amides are formed via a condensation reaction between a hydrocarbon-substituted succinic anhydride and an alkanolamine. Suitable alkanolamines include, for example, ethoxylated polyalkyl polyamines, propoxylated polyalkyl polyamines, and polyolefin polyamines such as polyethylene polyamines. One example is propoxylated hexamethylethylenediamine.

[0149] The hydrocarbon-substituted succinic anhydrides used in the preceding paragraphs typically have molecular weights in the range of 800 to 2,500 or greater. The products described above can undergo post-reactions with various reagents such as sulfur, oxygen, formaldehyde, and carboxylic acids like oleic acid. These products can also undergo post-reactions with boron compounds such as boric acid, borate esters, or highly borated dispersants to form borated dispersants that typically contain 0.1 to 5 moles of boron per mole of the reaction product.

[0150] Mannich base dispersants are prepared by reacting alkylphenols, formaldehyde, and amines. See U.S. Patent 4,767,551. Processing aids and catalysts such as oleic acid and sulfonic acid can also be part of the reaction mixture. The molecular weight of alkylphenols ranges from 800 to 2,500.

[0151] The Mannich condensate products used in the typical high molecular weight fatty acid modification of this invention can be prepared from high molecular weight alkyl-substituted hydroxy aromatic compounds or reactants containing HNR2 groups.

[0152] Example dispersants may include borated and unboronized succinimides, including succinimide derivatives derived from mono-succinimides, bis-succinimides, and / or mixtures of mono-succinimides and bis-succinimides, wherein the hydrocarbon succinimides are derived from: hydrocarbon subgroups, such as polyisobutylene with Mn of 500 to 5000, 1000 to 3000, or 1000 to 2000; or mixtures of such hydrocarbon subgroups, typically having high-terminated vinyl groups. Other dispersants include succinates and amides, alkylphenol-polyamine coupled Mannich adducts, their end-capped derivatives, and other related components.

[0153] Polymethyl methacrylate (PMMA) or polyacrylate derivatives are another class of dispersants. These dispersants are typically prepared by reacting a nitrogen-containing monomer with a PMMA or acrylate containing 5 to 25 carbon atoms in its ester group. Representative examples are shown in U.S. Patents 2,100,993 and 6,323,164. PMMA and polyacrylate dispersants are commonly used as multifunctional viscosity index improvers. Lower molecular weight versions can be used as lubricant dispersants or fuel cleaners.

[0154] In polar esters of non-aromatic dicarboxylic acids, such as adipates, polymethyl methacrylate or polyacrylate dispersants are preferred because many other conventional dispersants have poor solubility. Example dispersants for polyol esters in this invention may include polymethyl methacrylate and polyacrylate dispersants.

[0155] The amount of this dispersant can be from 0.1 to 20% by weight, for example, 0.5 to 8% by weight or 0.5 to 4% by weight. The hydrocarbon number of the dispersant atoms can be C10 or C20. 60 To C 1000 Or C 70 To C 300 Or C 70 To C 200 Within a certain range. These dispersants may contain both neutral nitrogen and basic nitrogen, or mixtures of both. The dispersants can be end-capped with borates and / or cyclic carbonates.

[0156] Other potential dispersants can include polyolefins, such as polyolefins with a molecular weight of at least 900 and an average of 1.3 to 1.7 functional groups per polyolefin moiety. Other suitable polymers can include those formed by cationic polymerization of monomers such as isobutylene and / or styrene.

[0157] Other additives - anti-wear agents

[0158] Metallic alkyl thiophosphates, and more particularly zinc dialkyl dithiophosphates or zinc dialkyl dithiophosphates (ZDDP), are useful components of the lubricants of the present invention. ZDDPs can be derived from primary alcohols, secondary alcohols, or mixtures thereof. ZDDP compounds typically have the following formula:

[0159] Zn[SP(S)(OR 1 (OR) 2 )]2

[0160] Where R 1 and R 2 It is C1-C 18 Alkyl groups, such as C2-C 12 Alkyl groups. These alkyl groups can be straight-chain or branched. The alcohols used in ZDDP can be 2-propanol, butanol, sec-butanol, pentanol, hexanol such as 4-methyl-2-pentanol, n-hexanol, n-octanol, 2-ethylhexanol, alkylated phenols, etc. Mixtures of secondary alcohols or mixtures of primary and secondary alcohols are preferred. Alkyl aryl groups can also be used.

[0161] Commercially available examples of zinc dithiophosphate include zinc secondary dithiophosphate, such as those commercially available from: The Lubrizol Corporation, trade names “LZ 677A”, “LZ 1095” and “LZ 1371”; Chevron Oronite, trade name “OLOA262”; and Afton Chemical, trade name “HITEC 7169”.

[0162] Based on the total weight of the lubricating oil, ZDDP is typically used in amounts from 0.4% to 1.2% by weight, for example from 0.5% to 1.0% by weight, for example from 0.6% to 0.8% by weight, but it can generally be used more or less advantageously. In some embodiments, ZDDP is secondary ZDDP and is present in an amount of 0.6% to 1.0% by weight of the total weight of the lubricating oil.

[0163] More generally, other suitable types of anti-wear additives can include metal salts of carboxylic acids, for example. The metal can be a transition metal or a mixture of transition metals, such as one or more metals derived from Groups 10, 11, or 12 of the IUPAC periodic table. The carboxylic acid can be an aliphatic carboxylic acid, a cyclic aliphatic carboxylic acid, an aromatic carboxylic acid, or a mixture thereof.

[0164] Low-phosphorus engine oil formulations are included in this invention. For such formulations, the phosphorus content is typically less than 0.12% by weight, for example less than 0.10% by weight or less than 0.085% by weight. Low phosphorus content may be preferred in combination with friction modifiers.

[0165] Other additives - extreme pressure additives

[0166] Extreme pressure additives can be incorporated into the fluids of the present invention. Extreme pressure additives may comprise organosulfur compounds, organophosphorus compounds, organoboron compounds, organosulfur-phosphorus compounds, organosulfur-phosphorus-boron compounds, organochlorine compounds, or any combination thereof. Some examples of such organic compounds include esters, triglycerides, alkanes, and alkenes. Suitable extreme pressure additives for the fluids of the present invention include temperature-dependent extreme pressure additives configured to react with metal surfaces under locally high-temperature conditions that may be present in a machine component, wherein one component of the machine component applies sufficient pressure to another component to create lubricating boundary conditions. Extreme pressure additives suitable for the fluids of the present invention include non-temperature-dependent extreme pressure additives. In some embodiments, the content of the extreme pressure additive in the fluids of the present invention may be from about 0.1 wt% to about 30 wt%, or from about 0.1 wt% to about 25 wt%, or from about 0.1 wt% to about 20 wt%.

[0167] Other additives - viscosity index improvers

[0168] Viscosity index improvers (also known as VI improvers, viscosity modifiers, and viscosity enhancers) can be included in the lubricant compositions of the present invention. Viscosity index improvers provide lubricants with high-temperature and low-temperature operability. These additives impart shear stability at high temperatures and acceptable viscosity at low temperatures.

[0169] Suitable viscosity index improvers include high molecular weight hydrocarbons, polyesters, and viscosity index improver dispersants that function as both viscosity index improvers and dispersants. These polymers typically have molecular weights of about 10,000 to 1,500,000, more typically about 20,000 to 1,200,000, and even more typically about 50,000 to 1,000,000. Polymethacrylate or polyacrylate viscosity index improvers typically have molecular weights of less than about 50,000.

[0170] Examples of suitable viscosity index improvers are linear or star-shaped polymers and copolymers of methacrylates, butadiene, olefins, or alkylated styrene. Polyisobutylene is a commonly used viscosity index improver. Another suitable viscosity index improver is polymethacrylate (e.g., copolymers of alkyl methacrylates of various chain lengths), some of which are also used as pour point depressants. Other suitable viscosity index improvers include copolymers of ethylene and propylene, hydrogenated block copolymers of styrene and isoprene, and polyacrylates (e.g., copolymers of acrylates of various chain lengths). Specific examples include styrene-isoprene or styrene-butadiene polymers with molecular weights from 50,000 to 200,000.

[0171] The olefin copolymer was purchased from Chevron Oronite Company LLC, under the trade name [not specified]. (For example" 8921 and " 8941”); Afton Chemical Corporation, product name (For example" 5850B”; and The Lubrizol Corporation, whose product name is “ 7067C". Hydrogenated polyisoprene star polymers are available from, for example, Infineum International Limited, under the trade names "SV200" and "SV600". Hydrogenated diene-styrene block copolymers are available from, for example, Infineum International Limited, under the trade name "SV 50".

[0172] In one embodiment of the invention, the amount of viscosity index improver used may be from 1.0 to 20% by weight, for example, from 5 to 15% by weight or from 8.0 to 12% by weight, based on the total weight of the formulated oil or lubricating engine oil.

[0173] Other additives - antioxidants

[0174] Antioxidants delay the oxidative degradation of base oils during use. This degradation can lead to deposits, sludge formation, or increased lubricant viscosity on metal surfaces. Those skilled in the art are aware of a variety of oxidation inhibitors that can be used in lubricant compositions.

[0175] Useful antioxidants include hindered phenols. These phenolic antioxidants can be ashless (metal-free) phenolic compounds or neutral or basic metal salts of specific phenolic compounds. Typical phenolic antioxidant compounds are sterically hindered phenolic compounds, which are compounds containing sterically hindered hydroxyl groups, and these compounds include those derivatives of dihydroxyaryl compounds in which the hydroxyl groups are located at ortho- or para-positions to each other. Typical phenolic antioxidants include those... 6+Stellated phenols substituted with alkyl groups and their alkylidene coupling derivatives. Examples of such phenols are 2-tert-butyl-4-heptylphenol, 2-tert-butyl-4-octylphenol, 2-tert-butyl-4-dodecylphenol, 2,6-di-tert-butyl-4-heptylphenol, 2,6-di-tert-butyl-4-dodecylphenol, 2-methyl-6-tert-butyl-4-heptylphenol, and 2-methyl-6-tert-butyl-4-dodecylphenol. Other useful sterically hindered monophenol antioxidants may include, for example, sterically hindered 2,6-dialkylphenol propionate derivatives. Bisphenol antioxidants may also be advantageously used in combination with the present invention. Examples of ortho-coupled phenols include 2,2'-bis(4-heptyl-6-tert-butylphenol), 2,2'-bis(4-octyl-6-tert-butylphenol), and 2,2'-bis(4-dodecyl-6-tert-butylphenol). Para-coupled bisphenols include, for example, 4,4'-bis(2,6-di-tert-butylphenol) and 4,4'-methyl-ylidene bis(2,6-di-tert-butylphenol).

[0176] An effective amount of one or more catalytic antioxidants may also be used. Catalytic antioxidants comprise: an effective amount of a) one or more oil-soluble polymetallic organometallic compounds; and an effective amount of b) one or more substituted N,N'-diaryl-o-phenylenediamine compounds or c) one or more sterically hindered phenolic compounds; or a combination of b) and c).

[0177] Available non-phenolic oxidation inhibitors include aromatic amine antioxidants, which can be used alone or in combination with phenolic compounds. Typical examples of non-phenolic antioxidants include alkylated and non-alkylated aromatic amines, such as those of formula R. 8 R 9 R 10 N-aryl monoamines, of which R 8 It is an aliphatic, aromatic, or substituted aromatic group, R 9 It is an aromatic or substituted aromatic group, and R 10 It is H, alkyl, aryl or R 11 S(O)xR 12 , where R 11 It is an alkylene, alkenylene, or arylalkylene group, R 12 It is a higher alkyl group or alkenyl, aryl, or alkylaryl group, and x is 0, 1, or 2. Aliphatic group R 8 It can contain 1 to 20 carbon atoms, for example, 6 to 12 carbon atoms. The aliphatic group is an aliphatic group. In some embodiments, R... 8 and R 9 All are aromatic groups or substituted aromatic groups, and the aromatic groups can be fused-ring aromatic groups, such as naphthyl. Aromatic group R 8 and R 9 It can be linked with other groups such as S.

[0178] Typical aromatic amine antioxidants have alkyl substituents with at least 6 carbon atoms. Examples of aliphatic groups include hexyl, heptyl, octyl, nonyl, and decyl. Typically, the aliphatic group will contain no more than 14 carbon atoms. Common types of amine antioxidants used in this composition include diphenylamine, phenylnaphthylamine, phenothiazine, iminodibenzyl, and diphenylphenyldiamine. Mixtures of two or more aromatic amines are also useful. Polymeric amine antioxidants can also be used. Specific examples of aromatic amine antioxidants that can be used in this invention include: p,p'-dioctyldiphenylamine, t-octylphenyl-α-naphthylamine, phenyl-α-naphthylamine, and p-octylphenyl-α-naphthylamine.

[0179] Exemplary amine antioxidants in this invention include polymeric amines or oligoamines, which are products of polymerization reactions of the following substances: one or more substituted or hydrocarbon-substituted diphenylamines; one or more unsubstituted or hydrocarbon-substituted phenylnaphthylamines; or one or more unsubstituted or hydrocarbon-substituted diphenylamines and one or more unsubstituted or hydrocarbon-substituted phenylnaphthylamines.

[0180] Polymeric or oligomeric amines are commercially available from Nyco SA under the trade name Nycoperf AO337. The polymeric or oligomeric amine antioxidant is present in an amount ranging from 0.5 to 10% by weight (active ingredient), for example, 2 to 5% by weight (active ingredient), excluding any unpolymerized aryl amines or any added antioxidants that may be present. Sulfated alkylphenols and their bases or alkaline earth metal salts are also useful antioxidants.

[0181] Exemplary antioxidants also include hindered phenols and aryl amines. These antioxidants can be used alone or in combination with each other. The amount of this additive can be from 0.01 to 5% by weight, for example, 0.01 to 1.5% by weight, 0.01 to 1.0% by weight, or 0.01 to 0.5% by weight.

[0182] Other additives - Pour point depressant (PPD)

[0183] If desired, one or more pour point depressants (also known as lubricant flow improvers) may be added to the compositions of the present invention. Pour point depressants may be added to the lubricating compositions of the present invention to lower the minimum temperature at which the fluid will flow or can be poured. Examples of suitable pour point depressants include alkyl polymethacrylates, polymethacrylates, polyacrylates, polyarylamides, acrylate-styrene copolymers, esterified olefin copolymers, alkylated polystyrene, vinyl acetate-fumarate copolymers, condensation products of haloparaffins and aromatic compounds, vinyl carboxylate polymers, and terpolymers of dialkyl fumarate, vinyl fatty acid esters, and allyl vinyl ethers. The amount of such additive may be from about 0.01 to 5% by weight, for example, from about 0.01 to 1.5% by weight.

[0184] Other additives - sealing compatibilizers

[0185] Sealing compatibilizers help swell resilient seals by inducing chemical reactions in fluids or physical changes in elastomers. Suitable sealing compatibilizers for lubricants include organophosphates, aromatic esters, aromatic hydrocarbons, esters (e.g., butyl benzyl phthalate), and polybutenyl succinic anhydride. The amount of such additive can be from about 0.01 to 3% by weight, for example, from about 0.01 to 2% by weight.

[0186] Other additives - defoamers

[0187] Defoamers can be advantageously added to lubricant compositions. These agents inhibit the formation of stable foam. Organosilicones and organic polymers are typical defoamers. For example, polysiloxanes such as silicone oil or polydimethylsiloxane provide defoaming properties. Defoamers are commercially available and can be used in conventional small amounts with other additives such as demulsifiers, typically in amounts less than 1% by weight and usually less than 0.1% by weight.

[0188] Other additives - inhibitors and rust inhibitors

[0189] Rust inhibitors (or corrosion suppressants) are additives that protect lubricated metal surfaces from chemical corrosion by water or other contaminants. Many of these additives are commercially available.

[0190] One type of rust inhibitor is a polar compound that preferentially wets the metal surface to protect it with an oil film. Another type of rust inhibitor absorbs moisture by being incorporated into a water-in-oil emulsion, so that only the oil comes into contact with the metal surface. Yet another type of rust inhibitor chemically adheres to the metal to create a non-reactive surface. Examples of suitable additives include zinc dithiophosphate, metal phenolates, basic metal sulfonates, fatty acids, and amines. The amount of such additives can be from about 0.01 to 5% by weight, for example, from about 0.01 to 1.5% by weight.

[0191] Other additives - friction modifiers

[0192] Friction modifiers are any one or more materials capable of altering the coefficient of friction of a surface lubricated by any lubricant or fluid containing such a material. If desired, friction modifiers, also known as friction reducers, lubricants, or oiliness agents, can be effectively combined with base oils or the lubricant compositions of the present invention; and other such agents that alter the ability of base oils, formulated lubricant compositions, or functional fluids to change the coefficient of friction of the lubricated surface. Friction modifiers that reduce the coefficient of friction are particularly advantageous when combined with base oils and the lubricant compositions of the present invention.

[0193] Exemplary friction modifiers may comprise, for example, organometallic compounds or materials or mixtures thereof. Exemplary organometallic friction modifiers that can be used in the lubricating engine oil formulations of the present invention include, for example, molybdenum amine, molybdenum diamine, organotungstate, molybdenum dithiocarbamate, molybdenum dithiophosphate, molybdenum amine complexes, molybdenum carboxylate, and mixtures thereof. Similar tungsten compounds may be preferred.

[0194] Other exemplary friction modifiers that can be used in the lubricating engine oil formulations of the present invention include, for example, alkoxylated fatty acid esters, alkanolamides, polyol fatty acid esters, borate-modified glycerol fatty acid esters, fatty alcohol ethers, and mixtures thereof.

[0195] Exemplary alkoxylated fatty acid esters include, for example, polyoxyethylene stearate, fatty acid polyethylene glycol ester, etc. These substances may include polyoxypropylene stearate, polyoxybutylene stearate, polyoxyethylene isostearate, polyoxypropylene isostearate, polyoxyethylene palmitate, etc.

[0196] Exemplary alkanolamides include, for example, diethyl alkanolamide of laurate and diethyl alkanolamide of palmitate. These substances may include diethyl alkanolamide of oleate, diethyl alkanolamide of stearate, diethyl alkanolamide of oleate, polyethoxylated hydrocarbon amide, polypropoxylated hydrocarbon amide, etc.

[0197] Exemplary polyol fatty acid esters include, for example: glyceryl monooleate; saturated mono-, di-, and tri-glyceryl esters; glyceryl monostearate, etc. These substances can include polyol esters, hydroxyl-containing polyol esters, etc.

[0198] Exemplary boronized glycerol fatty acid esters include, for example: boronized glycerol monooleate; boronized saturated mono-glycerol, di-glycerol, and tri-glycerol esters; boronized glycerol monostearate, etc. In addition to glycerol polyols, these substances may also include trimethylolpropane, pentaerythritol, sorbitan, etc. These esters may be polyol monocarboxylic acid esters, polyol dicarboxylic acid esters, and sometimes polyol tricarboxylic acid esters. Examples may include: glycerol monooleate, glycerol dioleate, glycerol trioleate, glycerol monostearate, glycerol distearate, and glycerol tristearate; and the corresponding glycerol monopalmitate, glycerol dipalmitate, and glycerol tripalmitate; and the corresponding isostearate, linoleate, etc. Sometimes, glycerol esters and mixtures containing any of these substances may be preferred. Polyols, especially ethoxylated, propoxylated, and butoxylated fatty acid esters using glycerol as an underlying polyol, may be preferred. Exemplary fatty alcohol ethers include, for example, stearyl ether, myristyl ether, etc. Alcohols, including those with 3 to 5 carbon atoms, can be ethoxylated, propoxylated, or butoxylated to form the corresponding aliphatic alkyl ethers. The base alcohol moiety can be stearyl, myristyl, or C5. 11 -C 13 Hydrocarbons, oil-based compounds, isooctadecyl compounds, etc.

[0199] The useful concentration of the friction modifier can range from 0.01 wt% to 5 wt%, or from about 0.1 wt% to about 2.5 wt%, or from about 0.1 wt% to about 1.5 wt%, or from about 0.1 wt% to about 1 wt%. The concentration of molybdenum-containing materials is typically described as molybdenum metal concentration. The favorable concentration range of Mo can be from 25 ppm to 2000 ppm or greater, and sometimes from 50 to 1500 ppm. All types of friction modifiers can be used alone or in mixtures with the materials of the present invention. Mixtures of two or more friction modifiers or mixtures of friction modifiers with alternative surfactants are also generally desirable.

[0200] When a fluid composition contains one or more additives, the various additives are blended into the composition in an amount sufficient to enable them to perform their intended function in the application. Additives are typically present as minor components in the finished lubricant composition, typically in amounts less than 50% by weight, for example less than about 30% by weight, and for example less than about 15% by weight, based on the total weight of the composition. Various additives are typically present in the finished lubricant composition in amounts of at least 0.01% by weight, for example at least 1% by weight, and for example at least 5% by weight. Some additives, such as detergent packets, may be present in the finished lubricant composition in amounts of at least 10% by weight. The amounts of additives that can be used in the finished lubricants of the present invention are shown in Table 3 below.

[0201] Many additives are shipped from additive manufacturers as concentrates, containing one or more additives and a certain amount of base oil diluent. Therefore, the weights in Table 3 below, and other quantities mentioned herein, refer to the amount of the active ingredient (i.e., the undiluted portion of the ingredient). The weight percentages (wt%) shown below are based on the total weight of the finished lubricant composition.

[0202] Table 3

[0203]

[0204] The aforementioned additives are generally available as commercially available materials. These additives can be added individually, but are usually combined with packages available from lubricant additive suppliers. Additive packages with various components, proportions, and properties are available; the appropriate package will be selected considering the necessary use of the final composition.

[0205] Because additives for many types of lubricants are typically supplied in pre-packaged mixtures, adjusting the relative amount of one additive in a finished engine oil lubricant usually involves similar adjustments to all other additives in a given additive package. This adjustment may negatively impact the effectiveness of at least some of the other additives. For example, a reduction in the amount of antioxidant can lead to a corresponding reduction in the amount of anti-wear additives, resulting in a fluid with less wear protection than before. However, it is anticipated that the performance advantages offered by formulating fluids using the Group II high-viscosity base oils of this invention instead of the existing Group I bright oils provide an opportunity to reformulate additive packages, allowing individual additives to be supplied in these reformulated packages in relative amounts different from the current additive packages. Therefore, it is expected that additive packages will be able to provide fluids to be formulated such that the aforementioned adjustments to the relative amounts of individual additives can be achieved without sacrificing other properties of the fluid.

[0206] Example finished fluid

[0207] The Group II high-viscosity base oils of the present invention are ideally suited as lubricant base oils without blending limitations. Furthermore, these lubricant base oils are compatible with lubricant additives used in lubricant formulations. The lubricant base oils of the present invention can be blended with other lubricant base oils to form finished lubricants. Useful co-based lubricant base oils include Group I, II, III, IV, and V base oils and natural gas synthetic (GTL) oils. One or more co-based oils can be blended into a lubricant composition containing, based on the total finished lubricant composition, 0.1 to 50% by weight, or 0.5 to 40% by weight, 1 to 35% by weight, or 2 to 30% by weight, or 5 to 25% by weight, or 10 to 20% by weight of the novel Group II high-viscosity base oils of the present invention.

[0208] Examples of the Class II high-viscosity base oils and fluid compositions of the present invention can be used for a variety of lubricant-related end uses, such as lubricants or greases for devices or equipment requiring lubrication of moving and / or interacting mechanical parts, components, or surfaces. Useful devices include engines and machines. The novel Class II high-viscosity base oils of the present invention are suitable for formulating automotive crankcase lubricants, automotive gear oils, transmission oils, marine cylinder oils, marine tubular piston engine oils, passenger car engine oils, commercial vehicle engine oils, hybrid vehicle lubricants, plug-in hybrid vehicle lubricants, battery electric vehicle lubricants, automotive greases, and many industrial lubricants, including but not limited to circulating lubricants, industrial gear lubricants, onshore wind turbine lubricants, offshore wind turbine lubricants, paper machine oils, industrial greases, compressor oils, pump oils, refrigeration lubricants, hydraulic lubricants, and metalworking fluids.

[0209] The four properties desired by lubricants for the applications listed above are oxidation stability, good deposit control, high viscosity index, and fluid rheology that facilitates pumping fluids at low temperatures.

[0210] Oxidation involves a chemical reaction between the lubricant and oxygen, leading to the formation of sludge and deposits, resulting in mechanical fouling. Furthermore, oxidation can adversely increase the viscosity of the lubricant. Therefore, lubricants with good oxidation stability have a longer service life than those with poor oxidation stability, allowing for longer oil change intervals and thus reducing downtime costs. Although certain additives can enhance the oxidation stability of lubricants, these additives are consumed during operation, meaning the effectiveness of a lubricant only lasts if sufficient additives are maintained in the lubricant. Therefore, it is desirable to formulate lubricants whose oxidation stability derives at least in part from the inherent properties of the lubricant base oil.

[0211] Deposit control properties involve a fluid's ability to prevent the unwanted deposition of oxidation products and other contaminants on component surfaces. Oxidation products comprise the products of reactions between oxygen and fluid additives such as anti-wear chemicals. Undesirable material deposits lead to fouling of components, thus the fluid is preferred to prevent such deposition. While a fluid may have good oxidative stability, this does not necessarily mean that the fluid will also have good deposit control. Oxidation involves a reaction between fluid components and oxidation, while deposition involves the occurrence of the products of these reactions. On one hand, deposit control can involve maintaining reaction products and other solid contaminants suspended in the fluid, which is typically achieved through the use of additives such as dispersants. Dispersants typically work by adhering to solid contaminant particles, such that dispersant molecules substantially surround each solid contaminant particle, thereby preventing particle aggregation. Thus, a dispersant remains effective only if unused dispersant molecules remain in the fluid. On the other hand, deposit control can involve the dissolution of reaction products and other solid contaminants in the fluid. Generally, fluids containing a larger proportion of aromatic hydrocarbons are more effective than fluids containing a smaller proportion of aromatic hydrocarbons in dissolving some reaction products and other solid contaminants. From the two aspects of deposition control mentioned above, it is expected that lubricants formulated with the ability to dissolve and / or prevent the aggregation and deposition of solid contaminants can be derived at least in part from the inherent properties of the lubricant base oil.

[0212] The viscosity index of a lubricant provides an indication of how much its viscosity changes with temperature. Lubricants with a high viscosity index exhibit less viscosity variation with temperature compared to those with a low viscosity index. Therefore, lubricants used in equipment operating under a wide range of environmental conditions, such as extreme high and low temperatures, should have a high viscosity index. While a high viscosity index can be achieved by adding viscosity index improvers to lubricant formulations, the use of such additives is not always beneficial. For example, technological advancements in engines, components, and pumps have led to smaller engines producing greater power, components operating at faster speeds, and smaller pumps generating higher pressures than their predecessors. These operational improvements place higher demands on lubricants, requiring them to operate effectively under higher temperatures, higher pressures, and more stringent shear conditions. For instance, a reduction gearbox may operate alongside rapidly rotating components, potentially causing harmful shearing of the viscosity index improver in the lubricant. Once the viscosity index improver molecule is sheared, it becomes ineffective, resulting in a deterioration in the lubricant's viscosity profile and performance, ultimately damaging the equipment. Therefore, it is desirable to formulate lubricants with a high viscosity index, which is at least partially derived from the inherent properties of the lubricant's base oil.

[0213] Cryogenic fluid rheology can be considered as involving "flowability" or "pumpability"—a measure of how easily (or how difficult) a fluid can be pumped at low temperatures. Cryogenic rheological properties are most critical for mechanical devices operating in cold environments, such as machines and vehicles, especially when such devices begin to move from a standstill. When stationary, a machine may not have lubricant effectively distributed to its moving parts, so the contact surfaces may experience a greater level of friction and wear during startup than during normal operation. This greater degree of friction and wear can negatively impact the machine's efficiency and lifespan. The lubricant's ability to resist this wear can be compromised at low temperatures. First, the viscosity of the lubricant tends to increase as the temperature decreases, making it difficult to distribute the lubricant effectively at low temperatures. Second, wax crystallization can occur in the lubricant at low temperatures, which can exacerbate the problem of effective distribution. Third, both of these effects hinder the migration of additive chemicals through the lubricant. Many anti-wear and extreme pressure additives designed to mitigate metal-to-metal wear work by reacting with the metal surface. Thus, the effectiveness of an additive depends at least in part on the additive in contact with the metal surface. The impediment to the migration of additives within the fluid inhibits their contact with the metal surface, thus making them less effective than when operating at higher temperatures.

[0214] To counteract these effects, lubricants can be formulated to be relatively easy to pump during cold starts of mechanical devices, allowing the lubricant and necessary additives to be effectively distributed to moving parts within a short time interval. A typical rheological property of a lubricant is its viscosity at low temperatures. Generally, the lower the viscosity at a given low temperature, the more effectively the lubricant distributes during machine startup, and the less harmful cold starts are to the equipment. For machines powered by battery electricity, such as motor vehicle engines, a problem arises where the energy required for starting at low temperatures is combined with the energy required to pump the high-viscosity lubricant fluid, but the battery's power output itself decreases at low temperatures. Therefore, lubricants with lower viscosity at low temperatures can at least partially compensate for the reduced power output of the battery at low temperatures.

[0215] While various additives can be used to enhance the low-temperature rheological properties of lubricants, this use can adversely affect other performance properties of the lubricant, such as viscosity index or oxidation resistance. Furthermore, increased use of additives often raises the cost of the lubricant. Therefore, it is desirable to formulate lubricants with improved low-temperature rheological properties, which are at least partially derived from the inherent properties of the lubricant base oil.

[0216] The various tests documented in the following examples provide a side-by-side performance comparison between lubricant fluids blended with the Group II high-viscosity base oils of the present invention and equivalent fluids blended with the Group I high-viscosity base oils. The performance comparisons include tests indicative of at least one of oxidation stability, deposit control, and low-temperature rheology. Each side-by-side comparison is performed where the only significant difference between the test fluids of each pair of examples is the type of high-viscosity base oil used in the blend. For some side-by-side comparisons, slight variations in the co-blended base oils as a minor component are necessary to obtain the equivalent viscosity properties of the side-by-side test samples. In each side-by-side comparison, the same amount of the same additive is blended into each fluid of the pair of examples of the comparison fluids in the same weight percentage. Thus, for each pair of comparative test samples, the total weight percentage of the base oil is the same, and the only significant difference between the two fluids in each pair is the use of the Group II high-viscosity base oils of the present invention in one fluid and the use of the Group I high-viscosity base oils in the other.

[0217] Regarding oxidation stability, the test results cited below indicate that fluids blended with the Group II high-viscosity base oils of this invention exhibit better oxidation stability than comparative fluids blended with Group I high-viscosity base oils. For Group I base oils, aromatic compound contents can lead to poor oxidation performance, but sulfur contents can contribute to better oxidation performance. The presence of sufficient antioxidant additives in the finished lubricants blended with Group I base oils provides acceptable oxidation stability. Although the Group II high-viscosity base oils of this invention lack the aromatic compound contents of Group I base oils, blends of the Group II high-viscosity base oils of this invention containing a significant amount of Group I base oils are expected to exhibit equivalent or slightly improved oxidation stability compared to comparative fluids blended solely with Group I base oils having the same antioxidant content. However, it has been found that the improvement in oxidation stability of fluids blended with the Group II high-viscosity base oils of this invention is significant.

[0218] Regarding deposit control, the test results cited below indicate that fluids blended with the Group II high-viscosity base oils of this invention exhibit similar deposit control capabilities to comparative fluids blended with Group I high-viscosity base oils. Group I base oils contain significantly more aromatic hydrocarbons than Group II base oils, particularly the Group II high-viscosity base oils of this invention. For a comparative pair of fluids containing the same proportions of the same additives, it can be expected that the fluid containing more aromatic hydrocarbons will exhibit better deposit control. Although the Group II high-viscosity base oils of this invention lack aromatic hydrocarbons, it has been found that fluids blended with the Group II high-viscosity base oils of this invention can have equivalent or better deposit control capabilities.

[0219] Regarding low-temperature rheology, the test results cited below demonstrate that fluids blended with the Group II high-viscosity base oils of this invention exhibit significantly superior low-temperature rheological properties compared to comparative fluids blended with Group I high-viscosity base oils. Although Group I base oils may contain more wax than the Group II high-viscosity base oils of this invention, it is expected that the additives used in the comparative tests will offset the effect of the wax present in the fluids blended with Group I base oils. For comparative pairs of fluids containing the same proportions of the same additives, it can be expected that wax crystallization is controlled by the additives, and thus the fluids blended with Group I high-viscosity base oils will exhibit similar (or only slightly inferior) low-temperature rheological properties compared to the fluids blended with Group II high-viscosity base oils of this invention. Despite the presence of an equivalent amount of wax-controlling additives in the comparative fluids blended with Group I high-viscosity base oils, it has been found that fluids blended with Group II high-viscosity base oils of this invention can possess excellent, particularly significantly excellent, low-temperature rheological properties.

[0220] The Group II high-viscosity base oils of this invention can be used to formulate fluids to help meet the aforementioned needs for oxidation stability, deposit control, high viscosity index, and appropriate cryogenic fluid rheology. For example, finished lubricant formulations containing the Group II high-viscosity base oils of this invention can have improved oxidation performance compared to existing comparative formulations, allowing end users to benefit from longer oil change intervals, thereby reducing equipment downtime and reducing operating expenses associated with lubricant discharge and replacement. Alternatively, finished lubricant formulations containing the Group II high-viscosity base oils of this invention and having a lower concentration of one or more additives compared to existing comparative formulations can achieve performance at least equivalent to existing comparative formulations. Replacing conventional Group I bright oils in finished lubricants with the Group II high-viscosity base oils of this invention can provide end users with at least equivalent operating performance while still meeting applicable health, safety, and / or environmental regulations.

[0221] Other benefits of finished lubricant formulations containing the Group II high-viscosity base oils of the present invention can be achieved when the lubricant is in a hotter environment or subjected to more severe operating conditions. Compared to existing comparative lubricant formulations, finished lubricant formulations containing the Group II high-viscosity base oils of the present invention can effectively reduce the amount of viscosity index improvers. Compared to existing comparative lubricant formulations, finished lubricant formulations containing the Group II high-viscosity base oils of the present invention can effectively reduce the amount of antioxidants. Furthermore, the improved low-temperature performance of finished lubricant formulations containing the Group II high-viscosity base oils of the present invention, compared to existing comparative formulations blended with Group I bright oils, allows for a reduction or even elimination of the pour point depressant treatment ratio. For example, although SAE grade 80W-90 automotive gear oils formulated with Group I bright oils typically contain 1.0 to 2.0% by weight of pour point depressants, equivalent formulations containing the Group II high-viscosity base oils of the present invention, replacing at least some of the Group I bright oils, can achieve comparable low-temperature performance with only 0.1 to 0.5% by weight of pour point depressants. For some high-viscosity automotive gear oils (e.g., SAE grade 85W-140) formulated with the Group II high-viscosity base oils of the present invention, the pour point lowering additive can be reduced to less than 0.1% by weight, less than 0.05% by weight, or eliminated. Furthermore, because finished lubricant formulations containing the Group II high-viscosity base oils of the present invention contribute to these properties, these finished lubricants can be more cost-effective compared to lubricants formulated with more expensive Group III, IV, and V base oils.

[0222] Correspondingly, methods for improving the oxidizing properties of fluids may involve blending a fluid using a Group II high-viscosity base oil of the present invention with one or more additives. The Group II high-viscosity base oil may have any one or more of the following: a viscosity index of at least 80, an aromatic compound content of less than 10% by weight, a sulfur content of less than 300 wppm, a kinematic viscosity of at least 14 cSt at 100°C, a kinematic viscosity of at least 320 cSt at 40°C, a pour point of -9°C or less, a cloud point of -2°C or less, or combinations thereof. According to ASTM D1401, the emulsification time of the Group II high-viscosity base oil at 82°C may be approximately 15 minutes. The total number of terminal / side-chain propyl groups and terminal / side-chain ethyl groups in the Group II high-viscosity base oil may be at least 1.7 per 100 carbon atoms. The aromatic compound content of the Group II high-viscosity base oil may be less than 8% by weight, less than 6% by weight, less than 4% by weight, or less than 2% by weight. Group II high-viscosity base oils may have a kinematic viscosity of at least 350 cSt, at least 400 cSt, at least 450 cSt, at least 500 cSt, or at least 550 cSt at 40°C. Group II high-viscosity base oils may have a T10 distillation point of at least 482°C.

[0223] The fluid may contain 20% or more, 30% or more, 40% or more, 50% or more, 60% or more, 70% or more, 75% or more, 80% or more, 85% or more, 90% or more, 93% or more, 95% or more, 97% or more, or 99% or more of Group II high-viscosity base oils. The fluid may have a saturated compound content of at least 60%, at least 70%, 80%, at least 85%, at least 90%, at least 95%, or at least 98% by weight. The fluid may have a KV100 increase of 6% or less, 5% or less, 4% or less, 3% or less, or about 2% as measured by ASTM D2893. The increase in the kinematic viscosity (KV100) of the fluid at 100°C, as measured according to the L-60-1 test bench test (ASTM D5704), can represent an oxidation property of 30% or less, 25% or less, 20% or less, or about 5% to 15%.

[0224] Alternatively or concurrently, the fluid may exhibit excellent deposit control performance. The fluid may have an average carbon / sludge grade of 8 to 10 as measured according to ASTM D5704, where 10 is the maximum grade under said test. The fluid may have an average sludge grade of 8 to 10 as measured according to ASTM D5704, where 10 is the maximum grade under said test. The fluid may have an average sludge grade of 9 to 10 as measured according to ASTM D5704.

[0225] Alternatively or alternatively, the fluid may have an antioxidant additive content of 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a viscosity index improver additive content of 10% by weight or less, 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a polyalphaolefin content of 10% by weight or less, 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a pour point depressant additive content of 5% by weight or less, 3% by weight or less, or 0.01% by weight to 1% by weight. In one embodiment, the fluid may be suitable for use as an automotive gear oil.

[0226] A method for improving the low-temperature rheological properties of a fluid may involve blending a fluid using a Group II high-viscosity base oil of the present invention with one or more additives. The Group II high-viscosity base oil may have any one or more of the following: a viscosity index of at least 80, an aromatic compound content of less than 10% by weight, a sulfur content of less than 300 wppm, a kinematic viscosity of at least 14 cSt at 100°C, a kinematic viscosity of at least 320 cSt at 40°C, a pour point of -9°C or less, a cloud point of -2°C or less, or combinations thereof. According to ASTM D1401, the emulsification time of the Group II high-viscosity base oil at 82°C may be approximately 15 minutes. The total number of terminal / side-chain propyl groups and terminal / side-chain ethyl groups in the Group II high-viscosity base oil may be at least 1.7 per 100 carbon atoms. The aromatic compound content of the Group II high-viscosity base oil may be less than 8% by weight, less than 6% by weight, less than 4% by weight, or less than 2% by weight. Group II high-viscosity base oils may have a kinematic viscosity of at least 350 cSt, at least 400 cSt, at least 450 cSt, at least 500 cSt, or at least 550 cSt at 40°C. Group II high-viscosity base oils may have a T10 distillation point of at least 482°C.

[0227] The fluid may contain 20% or more, 30% or more, 40% or more, 50% or more, 60% or more, 70% or more, 75% or more, 80% or more, 85% or more, 90% or more, 93% or more, 95% or more, 97% or more, or 99% or more of Group II high-viscosity base oils. The fluid may have a saturated compound content of at least 60% or at least 70% or 80% or at least 85% or at least 90% or at least 95% or at least 98% by weight.

[0228] According to ASTM D2983, the Brinell viscosity of a fluid at -12°C can be 70,000 mPa·s or less, 60,000 mPa·s or less, 50,000 mPa·s or less, 40,000 mPa·s or less, or 30,000 mPa·s to 40,000 mPa·s.

[0229] Alternatively or alternatively, the Brookfield viscosity of the above fluid at -26°C, as measured according to ASTM D2983, may be 150,000 mPa·s or less, 140,000 mPa·s or less, 130,000 mPa·s or less, 120,000 mPa·s or less, 110,000 mPa·s or less, 100,000 mPa·s or less, 90,000 mPa·s or less, 80,000 mPa·s or less, or 70,000 mPa·s to 80,000 mPa·s.

[0230] Alternatively or alternatively, the apparent viscosity of the fluid at -15°C, as measured according to ASTM D4684, may be 17,000 mPa·s or less, 16,000 mPa·s or less, 15,000 mPa·s or less, or 14,000 mPa·s to 15,000 mPa·s.

[0231] Alternatively or alternatively, the antioxidant additive content of the fluid may be 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a viscosity index improver additive content of 10% by weight or less, 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a polyalphaolefin content of 10% by weight or less, 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a pour point depressant additive content of 5% by weight or less, 3% by weight or less, or 0.01% by weight to 1% by weight. In one embodiment, the fluid is suitable for use as an automotive gear oil. In one embodiment, the fluid is suitable for use as an engine oil.

[0232] The Class II high-viscosity base oils of the present invention can be used to formulate fluids having any two or more of the following properties: oxidation stability, high viscosity index, and fluid rheology that facilitates pumping the fluid at low temperatures.

[0233] Therefore, methods for improving the life and performance of fluids may involve blending a fluid using the Group II high-viscosity base oil of the present invention with one or more additives. The Group II high-viscosity base oil may have any one or more of the following: a viscosity index of at least 80, an aromatic compound content of less than 10% by weight, a sulfur content of less than 300 wppm, a kinematic viscosity of at least 14 cSt at 100°C, a kinematic viscosity of at least 320 cSt at 40°C, a pour point of -9°C or less, a cloud point of -2°C or less, or combinations thereof. According to ASTM D1401, the emulsification time of the Group II high-viscosity base oil at 82°C may be approximately 15 minutes. The total number of terminal / side-chain propyl groups and terminal / side-chain ethyl groups in the Group II high-viscosity base oil may be at least 1.7 per 100 carbon atoms. The aromatic compound content of the Group II high-viscosity base oil may be less than 8% by weight, less than 6% by weight, less than 4% by weight, or less than 2% by weight. Group II high-viscosity base oils may have a kinematic viscosity of at least 350 cSt, at least 400 cSt, at least 450 cSt, at least 500 cSt, or at least 550 cSt at 40°C. Group II high-viscosity base oils may have a T10 distillation point of at least 482°C.

[0234] The fluid may contain 20% or more, 30% or more, 40% or more, 50% or more, 60% or more, 70% or more, 75% or more, 80% or more, 85% or more, 90% or more, 93% or more, 95% or more, 97% or more, or 99% or more of Group II high-viscosity base oils. The fluid may have a saturated compound content of at least 60%, at least 70%, 80%, at least 85%, at least 90%, at least 95%, or at least 98% by weight. The fluid may have a KV100 increase of 6% or less, 5% or less, 4% or less, 3% or less, or about 2% as measured by ASTM D2893. According to tests conducted on the L-60-1 test bench (ASTM D5704), the increase in KV100 of the fluid can be 30% or less, 25% or less, 20% or less, or approximately 5% to 15%.

[0235] Alternatively or concurrently, the fluid may exhibit excellent deposit control performance. The fluid may have an average carbon / sludge grade of 8 to 10 as measured according to ASTM D5704, where 10 is the maximum grade under said test. The fluid may have an average sludge grade of 8 to 10 as measured according to ASTM D5704, where 10 is the maximum grade under said test. The fluid may have an average sludge grade of 9 to 10 as measured according to ASTM D5704.

[0236] Alternatively or alternatively, the Brinell viscosity of the fluid at -12°C, as measured according to ASTM D2983, may be 70,000 mPa·s or less, 60,000 mPa·s or less, 50,000 mPa·s or less, 40,000 mPa·s or less, or 30,000 mPa·s to 40,000 mPa·s.

[0237] Alternatively or alternatively, the Brookfield viscosity of the above fluid at -26°C, as measured according to ASTM D2983, may be 150,000 mPa·s or less, 140,000 mPa·s or less, 130,000 mPa·s or less, 120,000 mPa·s or less, 110,000 mPa·s or less, 100,000 mPa·s or less, 90,000 mPa·s or less, 80,000 mPa·s or less, or 70,000 mPa·s to 80,000 mPa·s.

[0238] Alternatively or alternatively, the apparent viscosity of the fluid at -15°C, as measured according to ASTM D4684, may be 17,000 mPa·s or less, 16,000 mPa·s or less, 15,000 mPa·s or less, or 14,000 mPa·s to 15,000 mPa·s.

[0239] Alternatively or alternatively, the fluid may have an antioxidant additive content of 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a viscosity index improver additive content of 10% by weight or less, 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a polyalphaolefin content of 10% by weight or less, 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a pour point depressant additive content of 5% by weight or less, 3% by weight or less, or 0.01% by weight to 1% by weight. In one embodiment, the fluid may be suitable for use as an automotive gear oil. In one embodiment, the fluid may be suitable for use as an engine oil.

[0240] The fluids of the present invention suitable for use as industrial lubricants may contain about 90% by weight of the Group II high-viscosity base oil of the present invention, wherein the base oil has a saturated compound content of about 90% by weight (i.e., such that the fluid itself has a saturated compound content of at least 80% by weight). The Group II high-viscosity base oil may have any one or more of the following: a viscosity index of at least 80, an aromatic compound content of less than 10% by weight, a sulfur content of less than 300 wppm, a kinematic viscosity of at least 14 cSt at 100°C, a kinematic viscosity of at least 320 cSt at 40°C, a pour point of -9°C or less, a cloud point of -2°C or less, and combinations thereof. According to ASTM D1401, the emulsification time of the Group II high-viscosity base oil at 82°C may be about 15 minutes. The sum of the terminal / side-chain propyl groups and the terminal / side-chain ethyl groups of the Group II high-viscosity base oil may be at least 1.7 per 100 carbon atoms. The aromatic compound content of Group II high-viscosity base oils may be less than 8% by weight, less than 6% by weight, less than 4% by weight, or less than 2% by weight. The kinematic viscosity of Group II high-viscosity base oils at 40°C may be at least 350 cSt, at least 400 cSt, at least 450 cSt, at least 500 cSt, or at least 550 cSt. Group II high-viscosity base oils may have a T10 distillation point of at least 482°C.

[0241] The fluid may contain 20% or more, 30% or more, 40% or more, 50% or more, 60% or more, 70% or more, 75% or more, 80% or more, 85% or more, 90% or more, 93% or more, 95% or more, 97% or more, or 99% or more of Group II high-viscosity base oils. The fluid may have a saturated compound content of at least 85%, at least 90%, at least 95%, or at least 98% by weight. The fluid may have a KV100 increase of 6% or less, 5% or less, 4% or less, 3% or less, or approximately 2%, as measured by ASTM D2893.

[0242] Alternatively or alternatively, the fluid may have an antioxidant additive content of 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a viscosity index improver additive content of 10% by weight or less, 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a polyalphaolefin content of 10% by weight or less, 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a pour point depressant additive content of 5% by weight or less, 3% by weight or less, or 0.01% by weight to 1% by weight. In one embodiment, the fluid is suitable for use as an automotive gear oil. In one embodiment, the fluid is suitable for use as an industrial gear oil. In one embodiment, the fluid is suitable for use as a paper machine oil-type industrial gear oil.

[0243] The fluids of the present invention suitable for use as automotive gear oils may contain 20% or more, 30% or more, 40% or more, 50% or more, 60% or more, 70% or more, 75% or more, 80% or more, 85% or more, 90% or more, 93% or more, 95% or more, 97% or more, or 99% or more of Group II high-viscosity base oils. For example, the fluids of the present invention may contain about 70% by weight of the Group II high-viscosity base oils of the present invention, wherein the base oils have a saturated compound content of about 90% by weight (i.e., such that the fluid itself has a saturated compound content of at least 60% by weight). Group II high-viscosity base oils may have any one or more of the following: a viscosity index of at least 80, an aromatic compound content of less than 10% by weight, a sulfur content of less than 300 wppm, a kinematic viscosity of at least 14 cSt at 100°C, a kinematic viscosity of at least 320 cSt at 40°C, a pour point of -9°C or less, a cloud point of -2°C or less, or combinations thereof. According to ASTM D1401, the emulsification time of Group II high-viscosity base oils at 82°C may be approximately 15 minutes. The total sum of terminal / side-chain propyl groups and terminal / side-chain ethyl groups in Group II high-viscosity base oils may be at least 1.7 per 100 carbon atoms. The aromatic compound content of Group II high-viscosity base oils may be less than 8% by weight, less than 6% by weight, less than 4% by weight, or less than 2% by weight. The kinematic viscosity of Group II high-viscosity base oils at 40°C may be at least 350 cSt, at least 400 cSt, at least 450 cSt, at least 500 cSt, or at least 550 cSt. Group II high-viscosity base oils can have a T10 distillation point of at least 482°C.

[0244] The fluid may contain approximately 80% by weight or more, 85% by weight or more, 90% by weight or more, or 95% by weight or more of Group II high-viscosity base oils. The fluid may have a saturated compound content of at least 70% by weight, at least 80% by weight, at least 85% by weight, at least 90% by weight, or at least 95% by weight. The fluid may have a Brinell viscosity of 70,000 mPa·s or less, 60,000 mPa·s or less, 50,000 mPa·s or less, 40,000 mPa·s or less, or 30,000 mPa·s to 40,000 mPa·s at -12°C, as measured by ASTM D2983.

[0245] Alternatively or alternatively, the Brookfield viscosity of the above fluid at -26°C, as measured according to ASTM D2983, may be 150,000 mPa·s or less, 140,000 mPa·s or less, 130,000 mPa·s or less, 120,000 mPa·s or less, 110,000 mPa·s or less, 100,000 mPa·s or less, 90,000 mPa·s or less, 80,000 mPa·s or less, or 70,000 mPa·s to 80,000 mPa·s.

[0246] Alternatively or alternatively, the fluid may have an antioxidant additive content of 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a viscosity index improver additive content of 10% by weight or less, 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a polyalphaolefin content of 10% by weight or less, 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a pour point depressant additive content of 5% by weight or less, 3% by weight or less, or 0.01% by weight to 1% by weight. In one embodiment, the fluid may be suitable for use as an automotive gear oil.

[0247] The fluid of this invention is suitable for use as an engine oil. Engine oils are intended for use in gasoline and diesel engines and typically contain base oils and additives. Base oils are usually the main component in these fluids and therefore have a significant impact on the performance of the engine oil. Typically, the wide variety of engine oils available today contains blends of small amounts of individual lubricant base oils and individual additives. Engine oils typically contain 80% by weight or more of base oils, with the remainder being various additives. Engine oils may contain 85% by weight or more, 90% by weight or more, or 95% by weight or more of base oils. One or two or more base oils may be included. Typically, a higher proportion of Group II high-viscosity base oils will be used in higher viscosity engine oils. However, because base oils can contain multiple base oils, Group II high-viscosity base oils can also be blended into relatively lighter viscosity engine oil products. In this case, extreme bimodal blends can be obtained, where Group II high-viscosity base oils are blended with light base oils to obtain blended base oils within the desired viscosity range.

[0248] The fluid of this invention may contain 20% or more, 30% or more, or 40% or more of the Group II high-viscosity base oil of this invention. The Group II high-viscosity base oil may have a saturated compound content of about 90% or more. The Group II high-viscosity base oil may have any one or more of the following: a viscosity index of at least 80, an aromatic compound content of less than 10% by weight, a sulfur content of less than 300 wppm, a kinematic viscosity of at least 14 cSt at 100°C, a kinematic viscosity of at least 320 cSt at 40°C, a pour point of -9°C or less, a cloud point of -2°C or less, and combinations thereof. According to ASTM D1401, the emulsification time of the Group II high-viscosity base oil at 82°C may be about 15 minutes. The total number of terminal / side-chain propyl groups and terminal / side-chain ethyl groups in the Group II high-viscosity base oil may be at least 1.7 per 100 carbon atoms. The aromatic compound content of Group II high-viscosity base oils may be less than 8% by weight, less than 6% by weight, less than 4% by weight, or less than 2% by weight. The kinematic viscosity of Group II high-viscosity base oils at 40°C may be at least 350 cSt, at least 400 cSt, at least 450 cSt, at least 500 cSt, or at least 550 cSt. Group II high-viscosity base oils may have a T10 distillation point of at least 482°C.

[0249] The fluid may contain approximately 50% by weight or more, 60% by weight or more, or 70% by weight or more of Group II high-viscosity base oils. The fluid may have a saturated compound content of at least 80% by weight, at least 85% by weight, or at least 90% by weight. The apparent MRV viscosity of the fluid at -15°C, as measured according to ASTM D4684, may be 17,000 mPa·s or less, 16,000 mPa·s or less, 15,000 mPa·s or less, or 14,000 mPa·s to 15,000 mPa·s.

[0250] Alternatively or alternatively, the fluid may have an antioxidant additive content of 5% by weight or less, 2% by weight or less, or 0.01% by weight or more to 1% by weight. Alternatively or alternatively, the fluid may have a viscosity index improver additive content of 10% by weight or less, 5% by weight or less, 2% by weight or less, or 0.01% by weight or more to 1% by weight. Alternatively or alternatively, the fluid may have a polyalphaolefin content of 10% by weight or less, 5% by weight or less, 2% by weight or less, or 0.01% by weight or more to 1% by weight. Alternatively or alternatively, the fluid may have a pour point depressant additive content of 5% by weight or less, 3% by weight or less, or 0.01% by weight or more to 1% by weight. In one embodiment, the fluid may be suitable for use as an engine oil.

[0251] In another embodiment, the fluid of the present invention may contain 20% or more, 30% or more, or 40% or more of the Group II high-viscosity base oil of the present invention. The Group II high-viscosity base oil may have a saturated compound content of about 90% or more. The Group II high-viscosity base oil may have any one or more of the following: a viscosity index of at least 80, an aromatic compound content of less than 10% by weight, a sulfur content of less than 300 wppm, a kinematic viscosity of at least 14 cSt at 100°C, a kinematic viscosity of at least 320 cSt at 40°C, a pour point of -9°C or less, a cloud point of -2°C or less, and combinations thereof. According to ASTM D1401, the emulsification time of the Group II high-viscosity base oil at 82°C may be about 15 minutes. The sum of the terminal / side-chain propyl groups and the terminal / side-chain ethyl groups of the Group II high-viscosity base oil may be at least 1.7 per 100 carbon atoms. The aromatic compound content of Group II high-viscosity base oils may be less than 8% by weight, less than 6% by weight, less than 4% by weight, or less than 2% by weight. The kinematic viscosity of Group II high-viscosity base oils at 40°C may be at least 350 cSt, at least 400 cSt, at least 450 cSt, at least 500 cSt, or at least 550 cSt. Group II high-viscosity base oils may have a T10 distillation point of at least 482°C.

[0252] The fluid may contain approximately 50% by weight or more, 60% by weight or more, 70% by weight or more, 75% by weight or more, 80% by weight or more, 85% by weight or more, 90% by weight or more, or 95% by weight or more of Group II high viscosity base oils. The fluid may have a saturated compound content of at least 70% by weight, at least 80% by weight, at least 85% by weight, at least 90% by weight, or at least 95% by weight. As measured according to L-60-1 test bench testing (ASTM D5704), the fluid may have a KV100 increase of 30% or less, 25% or less, 20% or less, or approximately 5% to 15%.

[0253] Alternatively or alternatively, the fluid may have a carbon / sludge grade of 10 or less as measured by the L-60-1 bench test (ASTM D5704). Alternatively or alternatively, the aforementioned fluid may have a carbon / sludge grade of about 8 to about 9 as measured by the L-60-1 bench test (ASTM D5704). Alternatively or alternatively, the aforementioned fluid may have a sludge grade of 10 or less as measured by the L-60-1 bench test (ASTM D5704).

[0254] Alternatively or alternatively, the fluid may have an antioxidant additive content of 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a viscosity index improver additive content of 10% by weight or less, 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a polyalphaolefin content of 10% by weight or less, 5% by weight or less, 2% by weight or less, or 0.01% by weight to 1% by weight. Alternatively or alternatively, the fluid may have a pour point depressant additive content of 5% by weight or less, 3% by weight or less, or 0.01% by weight to 1% by weight. In one embodiment, the fluid may be suitable for use as an automotive gear oil.

[0255] In another embodiment, a method of manufacturing an anti-deposit fluid may include combining a base oil with one or more additives to form a blend fluid configured to resist the formation of deposits in an oxidizing environment. The base oil may have a viscosity index of at least 80 and a kinematic viscosity of at least 320 cSt at 40°C or at least 14 cSt at 100°C. The base oil may contain greater than or equal to about 90% by weight of a saturated compound, less than or equal to about 10% by weight of an aromatic compound, and at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms.

[0256] Alternatively or alternatively, the base oil may have a T10 distillation point of at least 482°C. Alternatively or alternatively, the base oil may have a pour point of -9°C or less and / or a cloud point of -2°C or less.

[0257] The blended fluid can be selected from: base oils, lubricants, process fluids, hydraulic fluids, industrial fluids, automotive fluids, and combinations thereof. The blended fluid can be configured to resist oxidation in an oxidizing environment. The oxidizing environment can include temperatures up to 250℉ (121°C), up to 302℉ (150°C), or up to 325℉ (163°C). The oxidizing environment can include air. The oxidizing environment can include water. The blended fluid can be configured to resist deposit formation for at least 50 hours at temperatures up to 325℉ (163°C) in the presence of a metallic reagent. The metallic reagent can be any one of copper, steel, iron, and combinations thereof.

[0258] Blends can be configured to maintain fluidity at low temperatures. The apparent MRV viscosity of blends at -15°C, as measured by ASTM D4684, can be 17,000 mPa·s or less, 16,000 mPa·s or less, 15,000 mPa·s or less, or 14,000 mPa·s to 15,000 mPa·s. Alternatively, as measured by ASTM D2983, blends at -12°C can have a Brinell viscosity of 70,000 mPa·s or less, 60,000 mPa·s or less, 50,000 mPa·s or less, 40,000 mPa·s or less, or 30,000 mPa·s to 40,000 mPa·s. Alternatively or alternatively, the blended fluid may have a Brinell viscosity of 150,000 mPa·s or less, 140,000 mPa·s or less, 130,000 mPa·s or less, 120,000 mPa·s or less, 110,000 mPa·s or less, 100,000 mPa·s or less, 90,000 mPa·s or less, 80,000 mPa·s or less, or 70,000 mPa·s to 80,000 mPa·s, as measured according to ASTM D2983, at -26°C.

[0259] In another embodiment, a method for reducing deposit formation may include introducing a base oil into a blend. The base oil may have a viscosity index of at least 80 and a kinematic viscosity of at least 320 cSt at 40°C or at least 14 cSt at 100°C. The base oil may contain greater than or equal to about 90% by weight of a saturated compound, less than or equal to about 10% by weight of an aromatic compound, and at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms. Adding a base oil to a blend can improve the blend's resistance to deposit formation in oxidizing environments.

[0260] Alternatively or alternatively, the base oils may have a T10 distillation point of at least 482°C. Alternatively or alternatively, the base oils may have a pour point of -9°C or less and / or a cloud point of -2°C or less.

[0261] The blend fluid can be selected from: base oils, lubricants, process fluids, hydraulic fluids, industrial fluids, automotive fluids, and combinations thereof. After introduction into the base oil, the blend fluid can be configured to resist oxidation in an oxidizing environment. The oxidizing environment can include temperatures up to 250℉ (121°C), 302℉ (150°C), or 325℉ (163°C). The oxidizing environment can include air. The oxidizing environment can include water. After introduction into the base oil, the blend fluid can be configured to resist deposit formation for at least 50 hours in the presence of a metallic reagent at temperatures up to 325℉ (163°C). The metallic reagent can be any one of copper, steel, iron, and combinations thereof.

[0262] In another embodiment, a method for mitigating deposit formation in equipment may include introducing a blended fluid into a metallic component of the equipment. The blended fluid may comprise a base oil and one or more additives. The base oil may have a viscosity index of at least 80 and a kinematic viscosity of at least 320 cSt at 40°C or at least 14 cSt at 100°C. The base oil may comprise greater than or equal to about 90% by weight of a saturated compound, less than or equal to about 10% by weight of an aromatic compound, and at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms. The blended fluid may be configured to resist deposit formation in oxidizing environments.

[0263] Alternatively or alternatively, the base oils may have a T10 distillation point of at least 482°C. Alternatively or alternatively, the base oils may have a pour point of -9°C or less and / or a cloud point of -2°C or less.

[0264] The blended fluid can be selected from: base oils, lubricants, process fluids, hydraulic fluids, industrial fluids, automotive fluids, and combinations thereof. The blended fluid can be configured to resist oxidation in an oxidizing environment. The oxidizing environment can include temperatures up to 250℉ (121°C), up to 302℉ (150°C), or up to 325℉ (163°C). The oxidizing environment can include air. The oxidizing environment can include water. The blended fluid can be configured to resist deposit formation for at least 50 hours at temperatures up to 325℉ (163°C) in the presence of a metallic reagent. The metallic reagent can be any one of copper, steel, iron, and combinations thereof.

[0265] In another embodiment, the anti-deposition fluid may comprise a base oil and one or more additives. The base oil may have a viscosity index of at least 80 and a kinematic viscosity of at least 320 cSt at 40°C or at least 14 cSt at 100°C. The base oil may comprise greater than or equal to about 90% by weight of a saturated compound, less than or equal to about 10% by weight of an aromatic compound, and at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms. The anti-deposition fluid may be configured to maintain fluidity in low-temperature environments and resist deposit formation in oxidizing environments.

[0266] Alternatively or alternatively, the base oil may have a T10 distillation point of at least 482°C. Alternatively or alternatively, the base oil may have a pour point of -9°C or less and / or a cloud point of -2°C or less.

[0267] The anti-deposit fluid can be selected from: base oils, lubricants, process fluids, hydraulic fluids, industrial fluids, automotive fluids, and combinations thereof. The anti-deposit fluid can be configured to resist oxidation in an oxidizing environment. The oxidizing environment can include temperatures up to 250℉ (121°C), up to 302℉ (150°C), or up to 325℉ (163°C). The oxidizing environment can include air. The oxidizing environment can include water. The anti-deposit fluid can be configured to resist deposit formation for at least 50 hours at temperatures up to 325℉ (163°C) in the presence of a metallic reagent. The metallic reagent can be any one of copper, steel, iron, and combinations thereof.

[0268] Anti-deposition fluids can be configured to maintain fluidity in cryogenic environments. The apparent MRV viscosity of an anti-deposition fluid at -15°C, as measured by ASTM D4684, can be 17,000 mPa·s or less, 16,000 mPa·s or less, 15,000 mPa·s or less, or 14,000 mPa·s to 15,000 mPa·s. Alternatively, as measured by ASTM D2983, an anti-deposition fluid at -12°C can have a Brinell viscosity of 70,000 mPa·s or less, 60,000 mPa·s or less, 50,000 mPa·s or less, 40,000 mPa·s or less, or 30,000 mPa·s to 40,000 mPa·s. Alternatively or alternatively, anti-deposition fluids may have a Brinell viscosity of 150,000 mPa·s or less, 140,000 mPa·s or less, 130,000 mPa·s or less, 120,000 mPa·s or less, 110,000 mPa·s or less, 100,000 mPa·s or less, 90,000 mPa·s or less, 80,000 mPa·s or less, or 70,000 mPa·s to 80,000 mPa·s, as measured according to ASTM D2983, at -26°C.

[0269] Example

[0270] The following examples demonstrate the aforementioned and other benefits of using Group II high-viscosity base oils instead of Group I base oils in the formulation of fluids. The performance of exemplary fluids blended with the Group II base oils of this invention was tested using a wide range of industry-standard benches and test rigs. Numerous performance advantages were observed in the formulations containing the novel Group II high-viscosity base oils compared to blends containing Group I base oils. Furthermore, other performance properties were observed to be at least equivalent to, and generally better than, those in blends containing Group I base oils.

[0271] In the following example, Group II high-viscosity base oils are derived from low-severity deasphalting of residual oil fractions to form deasphalted oil. The deasphalted oil undergoes demetallization, hydrotreating, hydrocracking, hydrodewaxing, and hydrorefining to produce high-saturation base oils with the same viscosity range as conventional Group I bright oils.

[0272] Example 1: Paper machine oil; US Steel Oxidation Test

[0273] In this embodiment, a paper machine oil (Sample 1) corresponding to ISO 320 specification formulated with a Group I bright base oil was tested and compared with an equivalent paper machine oil (Sample 2) corresponding to ISO 320 specification formulated with a Group II high viscosity base oil of the present invention. In this embodiment, the formulation of Sample 2 is very similar to that of Sample 1, except that the Group II high viscosity base oil of the present invention is used in Sample 2 instead of the Group I bright base oil in Sample 1. The amount of Group I heavy neutral base oil was fine-tuned to match the viscosity in the two formulation blends. Thus, the fluids of Samples 1 and 2 contain the same additives in the same proportions as the corresponding blended base oils. The sample compositions are provided in Table 4.

[0274] Table 4

[0275]

[0276] The benefits of oxidative stability of the samples were observed using the ASTM D2893 (American Steel Oxidation) test. This test demonstrates the oxidation resistance of industrial lubricants in the presence of high temperature and oxygen. The oil was subjected to temperatures ranging from 95 to 121°C for 312 hours. The kinematic viscosity (KV100) of the oil at 100°C was measured before and after the test; the increase in viscosity indicates the oil's oxidation resistance. Figure 1 The KV100 increase values ​​of two samples in this embodiment are illustrated. Sample 1 (a fluid blended with a Type I bright oil substrate) experienced a 7% KV100 increase, while Sample 2 (a fluid blended with a Type II high-viscosity base oil of the present invention) experienced only a 4% KV100 increase. The KV100 increase in this test was caused by oxidation of the tested lubricant. Therefore, the greater the observed KV100 increase, the lower the oxidation resistance of the tested lubricant. Thus, it is expected that the lubricant undergoing this test will exhibit a lower KV100 increase value. Here, Sample 2 experienced a much smaller KV100 increase than Sample 1, therefore Sample 2 is judged to have excellent oxidation stability. Given that the only difference between the formulations of Sample 1 and Sample 2 is the type of base oil, it can be concluded that the improved oxidation stability of Sample 2 is due to the use of the Type II high-viscosity base oil of the present invention in its formulation.

[0277] Example 2: Industrial gear oil; US steel oxidation test

[0278] In this embodiment, an industrial gear oil (Sample 3) formulated with a Group I brightener and conforming to ISO 460 specifications was tested and compared with the same industrial gear oil (Sample 4) formulated with a Group II high-viscosity base oil of the present invention. In this embodiment, the formulation of Sample 4 is very similar to that of Sample 3, except that the Group II high-viscosity base oil of the present invention is used in Sample 4 instead of the Group I brightener in Sample 3. The amount of Group I heavy neutral base oil was fine-tuned to match the viscosity in the two formulated blends. Thus, the fluids of Samples 3 and 4 contain the same additives in the same proportions as the corresponding blended base oils. The sample compositions are provided in Table 5.

[0279] Table 5

[0280]

[0281] The benefits of oxidative stability of the samples were observed using the ASTM D2893 (American Steel Oxidation) test. The test conditions were the same as those in Example 1. Figure 1 The KV100 increase values ​​of two samples in this embodiment are illustrated. Sample 3 (a fluid blended with a Type I bright oil substrate) experienced a 6% KV100 increase, while Sample 4 (a fluid blended with a Type II high-viscosity base oil of the present invention) experienced only a 2% KV100 increase. Thus, the KV100 increase experienced by Sample 4 is significantly less than that experienced by Sample 3, therefore Sample 4 is judged to have excellent oxidative stability. Given that the only difference in formulation between Sample 3 and Sample 4 is the type of base oil, it can be concluded that the improved oxidative stability of Sample 4 is due to the use of the Type II high-viscosity base oil of the present invention in its formulation.

[0282] Example 3: Automotive gear oil; Brinell viscosity test

[0283] In this embodiment, an 85W-140 grade automotive gear oil (sample 5) formulated with Group I bright oil was tested and compared with an equivalent 85W-140 grade automotive gear oil (sample 6) formulated with Group II high viscosity base oil. In this embodiment, the formulation of sample 6 is very similar to that of sample 5, except that the Group II high viscosity base oil of the present invention is used in sample 6 instead of the Group I bright oil in sample 5. The amount of Group I low viscosity base oil was fine-tuned to match the viscosity in the two formulation blends. Thus, the fluids of samples 5 and 6 contain the same additives in the same proportions as the corresponding blended base oils. Furthermore, in this embodiment, an 80W-90 grade automotive gear oil (sample 7) formulated with Group I bright oil was tested and compared with an equivalent 85W-140 grade automotive gear oil (sample 8) formulated with the Group II high viscosity base oil of the present invention. In this embodiment, the formulation of Sample 8 is very similar to that of Sample 7, except that the Group II high-viscosity base oil of the present invention is used in Sample 8 instead of the Group I bright oil of Sample 7. The amount of Group I low-viscosity base oil was fine-tuned to match the viscosity in the two formulated blends. Thus, the fluids of Samples 7 and 8 contain the same additives in the same proportions as the corresponding blended base oils. The sample compositions are provided in Table 6.

[0284] Table 6

[0285]

[0286] The low-temperature testing method used for automotive gear oils, automatic transmission fluids, torque and tractor fluids, as well as industrial and automotive hydraulic fluids, is the ASTM D2983 Brinell viscosity test. In this test, the sample is preheated and then brought to room temperature. The sample is then cooled to the specified test temperature and analyzed (alongside a reference fluid) by a rotational viscometer. The test determines the low shear rate viscosity of the sample at the specified test temperature. In this embodiment, samples 5 and 6 were tested at -12°C, and samples 7 and 8 were tested at -26°C.

[0287] Figure 2 The Brookfield viscosity values ​​of four samples from this embodiment are illustrated. Sample 5 (a fluid blended from a Type I bright oil substrate) has a Brookfield viscosity of 83,600 mPa·s, while Sample 6 (a fluid blended from a Type II high-viscosity base oil of the present invention) has a Brookfield viscosity of 31,800 mPa·s. Therefore, the Brookfield viscosity of Sample 6 is significantly lower than that of Sample 5, thus indicating that Sample 6 exhibits superior low-temperature performance. Given that the only difference between the formulations of Sample 5 and Sample 6 is the type of base oil, it can be concluded that the improved low-temperature performance of Sample 6 is due to the use of the Type II high-viscosity base oil of the present invention in its formulation.

[0288] Still refer to Figure 2 Sample 7 (a fluid blended from a Type I bright oil substrate) has a Brinell viscosity of 203,200 mPa·s, while Sample 8 (a fluid blended from a Type II high-viscosity base oil of the present invention) has a Brinell viscosity of 74,400 mPa·s. Therefore, the Brinell viscosity of Sample 8 is significantly lower than that of Sample 7, thus indicating that Sample 8 exhibits superior low-temperature performance. Given that the only difference between the formulations of Sample 7 and Sample 8 is the type of base oil, it can be concluded that the improved low-temperature performance of Sample 8 is due to the use of the Type II high-viscosity base oil of the present invention in its formulation.

[0289] Example 4: Automotive engine oil; MRV apparent viscosity test

[0290] In this embodiment, a 25W-50 engine oil (sample 9) formulated with a Group I bright oil was tested and compared with an equivalent 25W-50 engine oil (sample 10) formulated with a Group II high-viscosity base oil of the present invention. In this embodiment, the formulation of sample 10 is very similar to that of sample 9, except that the Group II high-viscosity base oil of the present invention is used in sample 10 instead of the Group I bright oil in sample 9. The amount of Group I low-viscosity base oil was fine-tuned to match the viscosity in the two formulation blends. Thus, the fluids of samples 9 and 10 contain the same additives in the same proportions as the corresponding base oils. The sample compositions are provided in Table 7.

[0291] Table 7

[0292]

[0293] The low-temperature test for engine oils is the ASTM D4684 Miniature Rotational Viscometer (MRV) apparent viscosity test. This is a critical test for automotive engine oils because it helps determine the viscosity grade and pumpability at low temperatures. The test is a low-temperature, low-shear test, in which the oil is slowly cooled and then subjected to a low-shear viscosity test. Samples 9 and 10 were cooled at a rate of 0.3°C / hour within the range of -8 to -20°C, within which most of the wax formation occurs. According to the SAE J300 engine oil classification standard, the test temperature for this 25W engine oil is -15°C, and a maximum MRV apparent viscosity of 60,000 mPa·s is the acceptable standard.

[0294] Figure 3The apparent MRV viscosity values ​​of two samples from this embodiment are illustrated. Sample 9 (a fluid blended from a Type I bright oil substrate) has an MRV apparent viscosity of 20,500 mPa·s at a test temperature of -15°C, while Sample 10 (a fluid blended from a Type II high-viscosity base oil of the present invention) has an MRV viscosity of 14,000 mPa·s at the same test temperature. Therefore, Sample 10 has a significantly lower MRV apparent viscosity than Sample 9, thus indicating that Sample 10 exhibits superior low-temperature performance. Given that the only difference between the formulations of Sample 9 and Sample 10 is the type of base oil, it can be concluded that the improved low-temperature performance of Sample 10 is due to the use of the Type II high-viscosity base oil of the present invention in its formulation.

[0295] Example 5: Automotive gear oil; tested on L-60-1 test bench

[0296] In this embodiment, an 85W-140 grade automotive gear oil (sample 11) formulated with Group I bright oil was tested for comparison with an equivalent 85W-140 grade automotive gear oil (sample 12) formulated with Group II high viscosity base oil. In this embodiment, the formulation of sample 12 was very similar to that of sample 11, except that the Group II high viscosity base oil of the present invention was used in place of the Group I bright oil in sample 11. The amount of Group I low viscosity base oil was fine-tuned to match the viscosity in the two formulation blends. Thus, the fluids of samples 11 and 12 contained the same additives in the same proportions as the corresponding base oils. Furthermore, in this embodiment, another 85W-140 grade automotive gear oil (sample 13) formulated with Group I bright oil was tested for comparison with another equivalent 85W-140 grade automotive gear oil (sample 14) formulated with the Group II high viscosity base oil of the present invention. In this embodiment, the formulation of sample 14 is identical to that of sample 13, except that the Group II high-viscosity base oil of the present invention is used in place of the Group I bright oil of sample 13 in sample 14. Thus, the fluids of samples 13 and 14 contain the same additives in the same proportions as the corresponding blended base oils. The sample compositions are provided in Table 8.

[0297] Table 8

[0298]

[0299] Samples 11, 12, 13, and 14 were tested on an L-60-1 test bench (ASTM D5704) to examine the thermal and oxidative stability of the automotive gear oils. The results of this test demonstrate the deposit control capabilities of the automotive gear oil formulation. In this test, the sample oil and catalyst were supplied to the gearbox, which was then heated to 325℉ (163℃) and run for 50 hours with the gears engaged. The kinematic viscosity (KV100) of the sample oil at 100℃ was measured before and after the test; the increase in viscosity indicates the oil's oxidation resistance. Figure 4 The KV100 increase values ​​of four samples in this embodiment are illustrated. Sample 11 (a fluid blended with a Type I bright oil substrate) experienced a 48% KV100 increase, while Sample 12 (a fluid blended with a Type II high-viscosity base oil of the present invention) experienced only an 11% KV100 increase. The KV100 increase in this test was caused by oxidation of the tested lubricant. Therefore, the greater the observed KV100 increase, the lower the oxidation resistance of the tested lubricant. Thus, it is expected that the lubricant undergoing this test will exhibit a lower KV100 increase value. Here, the KV100 increase experienced by Sample 12 is much smaller than that experienced by Sample 11, therefore Sample 12 is judged to have excellent oxidation stability. Given that the only difference in formulation between Sample 11 and Sample 12 is the type of base oil, it can be concluded that the improved oxidation stability of Sample 12 is due to the use of the Type II high-viscosity base oil of the present invention in its formulation.

[0300] Figure 4 The KV100 increase values ​​of samples 13 and 14 are also exemplified. Sample 13 (a fluid blended with a Type I bright oil substrate) experienced a 35% increase in KV100, while sample 14 (a fluid blended with a Type II high-viscosity base oil of the present invention) experienced only a 14% increase in KV100. The KV100 increase experienced by sample 14 is much smaller than that experienced by sample 11, therefore sample 14 is judged to have excellent oxidative stability. Given that the only difference in formulation between samples 13 and 14 is the type of base oil, it can be concluded that the improved oxidative stability of sample 14 is due to the use of the Type II high-viscosity base oil of the present invention in its formulation.

[0301] The results also provide some insight into the potential variations that may be expected between lubricants formulated from different batches of their components. For example, although both Sample 11 and Sample 13 were formulated from Group I bright oils and exhibited properties consistent with the 85W-140 category, L-60-1 test results indicated that Sample 11 experienced greater degradation than Sample 13. Similarly, Samples 12 and 14, both formulated from new Group II high-viscosity base oils, experienced varying degrees of degradation, although the difference here was less than that shown between Samples 11 and 13. Without being bound by any particular theory, it is believed that such differences between seemingly similar samples can be explained by any one or more different additive chemicals within the additive package, different concentrations of the additive package, and / or detailed compositional differences between the base oils.

[0302] Despite the above discussion, the results are consistent, because similar substitutions of the Group II high-viscosity base oils of the present invention for the Group I bright oils result in higher oxidative stability of the fluids.

[0303] The L-60-1 test bench also features two key deposit testing parameters: coke / sludge grade and sludge grade. Samples 11 (a fluid blended with a Group I bright oil substrate) and 12 (a fluid blended with a Group II high-viscosity base oil of the present invention) were compared in both grades. Because Sample 11 contains a larger proportion of aromatic compounds than Sample 12 due to its Group I bright oil substrate, it can be expected that Sample 11 will exhibit better coke / sludge and sludge grades. Without being bound by any particular theory, it is believed that the aromatic compounds found in Group I base oils provide dissolving power for early oxidation products and sludge, thus it is expected that the scarcity of aromatic compounds in the new Group II high-viscosity base oil substrate will lead to poorer deposit control. Nevertheless, as shown below... Figure 5 and 6 As shown, samples 11 and 12 exhibited nearly identical levels of carbon deposits / sludge and sediment. These results collectively demonstrate that lubricants formulated with the Group II high-viscosity base oils of this invention, instead of the Group I bright oil substrates, exhibit higher oxidation stability under conditions without any loss of deposit control. Therefore, lubricants formulated with the Group II high-viscosity base oils of this invention exhibit higher thermal stability than equivalent lubricants formulated with Group I bright oils.

[0304] Other implementation methods

[0305] The present invention also provides the following embodiments, each of which can be regarded as optionally including any alternative embodiments.

[0306] Implementation 1. A method comprising: blending a base oil and one or more additives to form a lubricating fluid, wherein: the base oil has a T10 distillation point of at least 482°C, a viscosity index of at least 80, and a kinematic viscosity of at least 320 cSt at 40°C or at least 14 cSt at 100°C; and comprises: greater than or equal to about 90% by weight of a saturated compound, less than or equal to about 10% by weight of an aromatic compound, and at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms; and the lubricating fluid has an oxidation performance represented by 30% or less of an increase in kinematic viscosity (KV100) at 100°C as measured according to ASTM D5704 or 6% or less of an increase in kinematic viscosity (KV100) at 100°C as measured according to ASTM D2893.

[0307] Implementation Method 2. The method according to any of the above embodiments, wherein the lubricating fluid has an oxidation performance represented by an increase of 20% or less in kinematic viscosity (KV100) at 100°C as measured according to ASTM D5704.

[0308] Implementation 3. The method according to any of the above embodiments, wherein the lubricating fluid has an oxidation performance represented by an increase of 15% or less in kinematic viscosity (KV100) at 100°C as measured according to ASTM D5704.

[0309] Embodiment 4. The method according to any of the above embodiments, wherein the lubricating fluid has an oxidation performance represented by an increase of 5% or less in kinematic viscosity (KV100) at 100°C as measured according to ASTM D2893.

[0310] Embodiment 5. The method according to any of the above embodiments, wherein the lubricating fluid has an oxidation performance represented by an increase of 4% or less in kinematic viscosity (KV100) at 100°C as measured according to ASTM D2893.

[0311] Embodiment 6. The method according to any of the above embodiments, wherein the lubricating fluid has an oxidation performance represented by an increase of 3% or less in kinematic viscosity (KV100) at 100°C as measured according to ASTM D2893.

[0312] Embodiment 7. The method according to any of the above embodiments, wherein the lubricating fluid has a Brinell viscosity of 70,000 mPa·s or less at -12°C, as measured by ASTM D2983.

[0313] Embodiment 8. The method according to any of the above embodiments, wherein the lubricating fluid has a Brinell viscosity of 60,000 mPa·s or less at -12°C, as measured according to ASTM D2983.

[0314] Embodiment 9. The method according to any of the above embodiments, wherein the lubricating fluid has a Brinell viscosity of 50,000 mPa·s or less at -12°C, as measured by ASTM D2983.

[0315] Embodiment 10. The method according to any of the above embodiments, wherein the lubricating fluid has a Brinell viscosity of 30,000 mPa·s to 40,000 mPa·s as measured according to ASTM D2983 at -12°C.

[0316] Embodiment 11. The method according to any of the above embodiments, wherein the lubricating fluid has a Brinell viscosity of 150,000 mPa·s or less as measured according to ASTM D2983 at -26°C.

[0317] Embodiment 12. The method according to any of the above embodiments, wherein the lubricating fluid has a Brinell viscosity of 140,000 mPa·s or less at -26°C, as measured by ASTM D2983.

[0318] Embodiment 13. The method according to any of the above embodiments, wherein the lubricating fluid has a Brinell viscosity of 130,000 mPa·s or less as measured according to ASTM D2983 at -26°C.

[0319] Embodiment 14. The method according to any of the above embodiments, wherein the lubricating fluid has a Brinell viscosity of 120,000 mPa·s or less at -26°C, as measured by ASTM D2983.

[0320] Embodiment 15. The method according to any of the above embodiments, wherein the lubricating fluid has a Brinell viscosity of 110,000 mPa·s or less as measured according to ASTM D2983 at -26°C.

[0321] Embodiment 16. The method according to any of the above embodiments, wherein the lubricating fluid has a Brinell viscosity of 100,000 mPa·s or less as measured according to ASTM D2983 at -26°C.

[0322] Embodiment 17. The method according to any of the above embodiments, wherein the lubricating fluid has a Brinell viscosity of 90,000 mPa·s or less at -26°C, as measured by ASTM D2983.

[0323] Embodiment 18. The method according to any of the above embodiments, wherein the lubricating fluid has a Brinell viscosity of 80,000 mPa·s or less at -26°C, as measured by ASTM D2983.

[0324] Embodiment 19. The method according to any of the above embodiments, wherein the lubricating fluid has a Brinell viscosity of 70,000 mPa·s to 100,000 mPa·s as measured according to ASTM D2983 at -26°C.

[0325] Embodiment 20. The method according to any of the above embodiments, wherein the lubricating fluid has a pour point depressant additive content of 0.7% by weight or less.

[0326] Embodiment 21. The method according to any of the above embodiments, wherein the lubricating fluid has a pour point depressant additive content of 0.3% by weight or less.

[0327] Embodiment 22. The method according to any of the above embodiments, wherein the lubricating fluid has a polyalphaolefin content of 10% by weight or less.

[0328] Embodiment 23. The method according to any of the above embodiments, wherein the lubricating fluid has a polyalphaolefin content of 5% by weight or less.

[0329] Embodiment 24. The method according to any of the above embodiments, wherein the lubricating fluid has a polyalphaolefin content of 0.01% to 1% by weight.

[0330] Implementation 25. The method according to any of the above embodiments, wherein the base oil has a viscosity index of 80 to 120.

[0331] Embodiment 26. The method according to any of the above embodiments, wherein the lubricating fluid has a viscosity index improver additive content of 5% by weight or less.

[0332] Embodiment 27. The method according to any of the above embodiments, wherein the lubricating fluid has a viscosity index improver additive content of 0.01% to 1% by weight.

[0333] Embodiment 28. The method according to any of the above embodiments, wherein the lubricating fluid has a viscosity index improver additive selected from: polyacrylate, polymers of methacrylate, polymers of butadiene, polymers of olefins, polymers of alkylated styrene, copolymers of methacrylate, copolymers of butadiene, copolymers of olefins, copolymers of alkylated styrene, copolymers of ethylene, copolymers of propylene, block copolymers of hydrogenated styrene, block copolymers of hydrogenated isoprene, and combinations thereof.

[0334] Embodiment 29. The method according to any of the above embodiments, wherein the lubricating fluid has a saturated compound content of at least 70% by weight.

[0335] Embodiment 30. The method according to any of the above embodiments, wherein the lubricating fluid has a saturated compound content of at least 80% by weight.

[0336] Embodiment 31. The method according to any of the above embodiments, wherein the lubricating fluid has an antioxidant additive content of 0.1% by weight or less.

[0337] Embodiment 32. The method according to any of the above embodiments, wherein the lubricating fluid has an antioxidant additive content of 0.01% to 0.05% by weight.

[0338] Embodiment 33. The method according to any of the above embodiments, wherein the lubricating fluid is automotive gear oil.

[0339] Implementation 34. The method according to any of the above embodiments, wherein the lubricating fluid is engine oil.

[0340] Embodiment 35. The method according to any of the above embodiments, wherein the lubricating fluid is industrial gear oil.

[0341] Implementation 36. A method comprising: blending a base oil and one or more additives to form a lubricating fluid, wherein: the base oil has a T10 distillation point of at least 482°C, a viscosity index of at least 80, and a kinematic viscosity of at least 320 cSt at 40°C or at least 14 cSt at 100°C; and comprises: greater than or equal to about 90% by weight of a saturated compound, less than or equal to about 10% by weight of an aromatic compound, and at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms; and the lubricating fluid has a Brinell viscosity as measured according to ASTM D2983: 70,000 mPa·s or less at -12°C or 150,000 mPa·s or less at -26°C; or the lubricating fluid has an MRV viscosity of 18,000 mPa·s or less as measured according to ASTM D4684 at a test temperature of -20°C to -8°C.

[0342] Embodiment 37. The method according to Embodiment 36, wherein the lubricating fluid has a Brinell viscosity of 60,000 mPa·s or less at -12°C, as measured by ASTM D2983.

[0343] Embodiment 38. The method according to any one of Embodiments 36 to 37, wherein the lubricating fluid has a Brinell viscosity of 50,000 mPa·s or less at -12°C, as measured by ASTM D2983.

[0344] Embodiment 39. The method according to any one of Embodiments 36 to 38, wherein the lubricating fluid has a Brinell viscosity of 30,000 mPa·s to 40,000 mPa·s as measured according to ASTM D2983 at -12°C.

[0345] Embodiment 40. The method according to any one of Embodiments 36 to 39, wherein the lubricating fluid has a Brinell viscosity of 150,000 mPa·s or less at -26°C, as measured by ASTM D2983.

[0346] Embodiment 41. The method according to any one of Embodiments 36 to 40, wherein the lubricating fluid has a Brinell viscosity of 140,000 mPa·s or less at -26°C, as measured by ASTM D2983.

[0347] Embodiment 42. The method according to any one of Embodiments 36 to 41, wherein the lubricating fluid has a Brinell viscosity of 130,000 mPa·s or less as measured according to ASTM D2983 at -26°C.

[0348] Embodiment 43. The method according to any one of Embodiments 36 to 42, wherein the lubricating fluid has a Brinell viscosity of 120,000 mPa·s or less as measured by ASTM D2983 at -26°C.

[0349] Embodiment 44. The method according to any one of Embodiments 36 to 43, wherein the lubricating fluid has a Brinell viscosity of 110,000 mPa·s or less at -26°C, as measured by ASTM D2983.

[0350] Embodiment 45. The method according to any one of Embodiments 36 to 44, wherein the lubricating fluid has a Brinell viscosity of 100,000 mPa·s or less at -26°C, as measured by ASTM D2983.

[0351] Embodiment 46. The method according to any one of Embodiments 36 to 45, wherein the lubricating fluid has a Brinell viscosity of 90,000 mPa·s or less at -26°C, as measured by ASTM D2983.

[0352] Embodiment 47. The method according to any one of Embodiments 36 to 46, wherein the lubricating fluid has a Brinell viscosity of 80,000 mPa·s or less as measured according to ASTM D2983 at -26°C.

[0353] Embodiment 48. The method according to any one of Embodiments 36 to 47, wherein the lubricating fluid has a Brinell viscosity of 70,000 mPa·s to 100,000 mPa·s measured at -26°C according to ASTM D2983.

[0354] Example 49. The method according to Example 36, wherein the lubricating fluid has an MRV viscosity of 17,000 mPa·s or less as measured by ASTM D4684 at the test temperature.

[0355] Example 50. The method according to any one of Examples 36 and 49, wherein the lubricating fluid has an MRV viscosity of 16,000 mPa·s or less as measured according to ASTM D4684 at the test temperature.

[0356] Embodiment 51. The method according to any one of Embodiments 36, 49 and 50, wherein the lubricating fluid has an MRV viscosity of 14,000 mPa·s to 15,000 mPa·s as measured according to ASTM D4684 at the test temperature.

[0357] Embodiment 52. The method according to any one of Embodiments 36 to 51, wherein the lubricating fluid has a pour point depressant additive content of 0.7% by weight or less.

[0358] Embodiment 53. The method according to any one of Embodiments 36 to 52, wherein the lubricating fluid has a pour point depressant additive content of 0.3% by weight or less.

[0359] Embodiment 54. The method according to any one of Embodiments 36 to 53, wherein the lubricating fluid has a polyalphaolefin content of 10% by weight or less.

[0360] Embodiment 55. The method according to any one of Embodiments 36 to 54, wherein the lubricating fluid has a polyalphaolefin content of 5% by weight or less.

[0361] Embodiment 56. The method according to any one of Embodiments 36 to 55, wherein the lubricating fluid has a polyalphaolefin content of 0.01% to 1% by weight.

[0362] Embodiment 57. The method according to any one of Embodiments 36 to 56, wherein the base oil has a viscosity index of 80 to 120.

[0363] Embodiment 58. The method according to any one of Embodiments 36 to 57, wherein the lubricating fluid has a viscosity index improver additive content of 5% by weight or less.

[0364] Embodiment 59. The method according to any one of Embodiments 36 to 58, wherein the lubricating fluid has a viscosity index improver additive content of 0.01% to 1% by weight.

[0365] Embodiment 60. The method according to any one of Embodiments 36 to 59, wherein the lubricating fluid has a viscosity index improver additive selected from: polyacrylate, polymers of methacrylate, polymers of butadiene, polymers of olefins, polymers of alkylated styrene, copolymers of methacrylate, copolymers of butadiene, copolymers of olefins, copolymers of alkylated styrene, copolymers of ethylene, copolymers of propylene, block copolymers of hydrogenated styrene, block copolymers of hydrogenated isoprene, and combinations thereof.

[0366] Embodiment 61. The method according to any one of Embodiments 36 to 60, wherein the lubricating fluid has a saturated compound content of at least 70% by weight.

[0367] Embodiment 62. The method according to any one of Embodiments 36 to 61, wherein the lubricating fluid has a saturated compound content of at least 80% by weight.

[0368] Embodiment 63. The method according to any one of Embodiments 36 to 62, wherein the lubricating fluid has an antioxidant additive content of 0.1% by weight or less.

[0369] Embodiment 64. The method according to any one of Embodiments 36 to 63, wherein the lubricating fluid has an antioxidant additive content of 0.01% to 0.05% by weight.

[0370] Embodiment 65. The method according to any one of Embodiments 36 to 64, wherein the lubricating fluid is automotive gear oil.

[0371] Embodiment 66. The method according to any one of Embodiments 36 to 64, wherein the lubricating fluid is engine oil.

[0372] Embodiment 67. The method according to any one of Embodiments 36 to 64, wherein the lubricating fluid is industrial gear oil.

[0373] Embodiment 68. A lubricating fluid comprising: a base oil and one or more additives, wherein: the base oil has a T10 distillation point of at least 482°C, a viscosity index of at least 80, and a kinematic viscosity of at least 320 cSt at 40°C or at least 14 cSt at 100°C; and comprises: greater than or equal to about 90% by weight of a saturated compound, less than or equal to about 10% by weight of an aromatic compound, and at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms; and the lubricating fluid has an oxidation performance represented by an increase of 30% or less in the kinematic viscosity (KV100) at 100°C as measured according to ASTM D5704, or an oxidation performance represented by an increase of 6% or less in the kinematic viscosity (KV100) at 100°C as measured according to ASTM D2893.

[0374] Embodiment 69. The lubricating fluid according to Embodiment 68, wherein the lubricating fluid has an oxidation property of 20% or less at 100°C, represented by an increase in kinematic viscosity (KV100) as measured according to ASTM D5704.

[0375] Embodiment 70. A lubricating fluid according to any one of Embodiments 68 to 69, wherein the lubricating fluid has an oxidation property of 15% or less at 100°C, represented by an increase in kinematic viscosity (KV100) as measured according to ASTM D5704.

[0376] Embodiment 71. A lubricating fluid according to any one of Embodiments 68 to 70, wherein the lubricating fluid has oxidation properties at 100°C represented by an increase of 5% or less in kinematic viscosity (KV100) as measured according to ASTM D2893.

[0377] Embodiment 72. A lubricating fluid according to any one of Embodiments 68 to 71, wherein the lubricating fluid has an oxidation property of 4% or less at 100°C, represented by an increase in kinematic viscosity (KV100) as measured according to ASTM D2893.

[0378] Embodiment 73. A lubricating fluid according to any one of Embodiments 68 to 72, wherein the lubricating fluid has oxidation properties at 100°C represented by an increase of 3% or less in kinematic viscosity (KV100) as measured according to ASTM D2893.

[0379] Embodiment 74. The lubricating fluid according to Embodiments 68 to 73, wherein the lubricating fluid has a Brinell viscosity of 70,000 mPa·s or less, measured at -12°C according to ASTM D2983.

[0380] Embodiment 75. The lubricating fluid according to Embodiments 68 to 74, wherein the lubricating fluid has a Brinell viscosity of 60,000 mPa·s or less, measured at -12°C according to ASTM D2983.

[0381] Embodiment 76. The lubricating fluid according to Embodiments 68 to 75, wherein the lubricating fluid has a Brinell viscosity of 50,000 mPa·s or less, measured at -12°C according to ASTM D2983.

[0382] Embodiment 77. The lubricating fluid according to Embodiments 68 to 76, wherein the lubricating fluid has a Brinell viscosity of 30,000 mPa·s to 40,000 mPa·s at -12°C, as measured according to ASTM D2983.

[0383] Embodiment 78. The lubricating fluid according to Embodiments 68 to 77, wherein the lubricating fluid has a Brinell viscosity of 150,000 mPa·s or less at -26°C, as measured according to ASTM D2983.

[0384] Embodiment 79. The lubricating fluid according to Embodiments 68 to 78, wherein the lubricating fluid has a Brinell viscosity of 140,000 mPa·s or less at -26°C, as measured according to ASTM D2983.

[0385] Embodiment 80. The lubricating fluid according to Embodiments 68 to 79, wherein the lubricating fluid has a Brinell viscosity of 130,000 mPa·s or less at -26°C, as measured according to ASTM D2983.

[0386] Embodiment 81. The lubricating fluid according to Embodiments 68 to 80, wherein the lubricating fluid has a Brinell viscosity of 120,000 mPa·s or less at -26°C, as measured according to ASTM D2983.

[0387] Embodiment 82. The lubricating fluid according to Embodiments 68 to 81, wherein the lubricating fluid has a Brinell viscosity of 110,000 mPa·s or less at -26°C as measured according to ASTM D2983.

[0388] Embodiment 83. The lubricating fluid according to Embodiments 68 to 82, wherein the lubricating fluid has a Brinell viscosity of 100,000 mPa·s or less at -26°C, as measured according to ASTM D2983.

[0389] Embodiment 84. The lubricating fluid according to Embodiments 68 to 83, wherein the lubricating fluid has a Brinell viscosity of 90,000 mPa·s or less at -26°C as measured according to ASTM D2983.

[0390] Embodiment 85. The lubricating fluid according to Embodiments 68 to 84, wherein the lubricating fluid has a Brinell viscosity of 80,000 mPa·s or less at -26°C as measured according to ASTM D2983.

[0391] Embodiment 86. The lubricating fluid according to Embodiments 68 to 85, wherein the lubricating fluid has a Brinell viscosity of 70,000 mPa·s to 100,000 mPa·s at -26°C, as measured according to ASTM D2983.

[0392] Embodiment 87. The lubricating fluid according to Embodiments 68 to 86, wherein the lubricating fluid has a pour point depressant additive content of 0.7% by weight or less.

[0393] Embodiment 88. The lubricating fluid according to Embodiments 68 to 87, wherein the lubricating fluid has a pour point depressant additive content of 0.3% by weight or less.

[0394] Embodiment 89. The lubricating fluid according to Embodiments 68 to 88, wherein the lubricating fluid has a polyalphaolefin content of 10% by weight or less.

[0395] Embodiment 90. The lubricating fluid according to Embodiments 68 to 89, wherein the lubricating fluid has a polyalphaolefin content of 5% by weight or less.

[0396] Embodiment 91. The lubricating fluid according to Embodiments 68 to 90, wherein the lubricating fluid has a polyalphaolefin content of 0.01% to 1% by weight.

[0397] Embodiment 92. The lubricating fluid according to Embodiments 68 to 91, wherein the base oil has a viscosity index of 100 to 120.

[0398] Embodiment 93. The lubricating fluid according to Embodiments 68 to 92, wherein the lubricating fluid has a viscosity index improver additive content of 5% by weight or less.

[0399] Embodiment 94. The lubricating fluid according to Embodiments 68 to 93, wherein the lubricating fluid has a viscosity index improver additive content of 0.01% to 1% by weight.

[0400] Embodiment 95. The lubricating fluid according to Embodiments 68 to 94, wherein the lubricating fluid has a viscosity index improver additive selected from: polyacrylate, polymers of methacrylate, polymers of butadiene, polymers of olefins, polymers of alkylated styrene, copolymers of methacrylate, copolymers of butadiene, copolymers of olefins, copolymers of alkylated styrene, copolymers of ethylene, copolymers of propylene, block copolymers of hydrogenated styrene, block copolymers of hydrogenated isoprene, and combinations thereof.

[0401] Embodiment 96. The lubricating fluid according to Embodiments 68 to 95, wherein the lubricating fluid has a saturated compound content of at least 70% by weight.

[0402] Embodiment 97. The lubricating fluid according to Embodiments 68 to 96, wherein the lubricating fluid has a saturated compound content of at least 80% by weight.

[0403] Embodiment 98. The lubricating fluid according to Embodiments 68 to 97, wherein the lubricating fluid has an antioxidant additive content of 0.1% by weight or less.

[0404] Embodiment 99. The lubricating fluid according to Embodiments 68 to 98, wherein the lubricating fluid has an antioxidant additive content of 0.01% to 0.05% by weight.

[0405] Embodiment 100. The lubricating fluid according to Embodiments 68 to 99, wherein the lubricating fluid is automotive gear oil.

[0406] Embodiment 101. The lubricating fluid according to Embodiments 68 to 100, wherein the lubricating fluid is engine oil.

[0407] Embodiment 102. The lubricating fluid according to Embodiments 68 to 101, wherein the lubricating fluid is industrial gear oil.

[0408] Embodiment 103. A lubricating fluid comprising: a base oil and one or more additives, wherein: the base oil has a T10 distillation point of at least 482°C, a viscosity index of at least 80, and a kinematic viscosity of at least 320 cSt at 40°C or at least 14 cSt at 100°C; and comprises: greater than or equal to about 90% by weight of a saturated compound, less than or equal to about 10% by weight of an aromatic compound, and at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms; and the lubricating fluid has a Brinell viscosity as measured according to ASTM D2983: 70,000 mPa·s or less at -12°C or 150,000 mPa·s or less at -26°C; or the lubricating fluid has an MRV viscosity of 18,000 mPa·s or less as measured according to ASTM D4684 at a test temperature of -20°C to -8°C.

[0409] Embodiment 104. The lubricating fluid according to Embodiment 103, wherein the lubricating fluid has a Brinell viscosity of 60,000 mPa·s or less at -12°C, as measured according to ASTM D2983.

[0410] Embodiment 105. A lubricating fluid according to any one of Embodiments 103 to 104, wherein the lubricating fluid has a Brinell viscosity of 50,000 mPa·s or less at -12°C as measured according to ASTM D2983.

[0411] Embodiment 106. A lubricating fluid according to any one of Embodiments 103 to 105, wherein the lubricating fluid has a Brinell viscosity of 30,000 mPa·s to 40,000 mPa·s at -12°C, as measured according to ASTM D2983.

[0412] Embodiment 107. A lubricating fluid according to any one of Embodiments 103 to 106, wherein the lubricating fluid has a Brinell viscosity of 150,000 mPa·s or less at -26°C, as measured according to ASTM D2983.

[0413] Embodiment 108. A lubricating fluid according to any one of Embodiments 103 to 107, wherein the lubricating fluid has a Brinell viscosity of 140,000 mPa·s or less at -26°C as measured according to ASTM D2983.

[0414] Embodiment 109. A lubricating fluid according to any one of Embodiments 103 to 108, wherein the lubricating fluid has a Brinell viscosity of 130,000 mPa·s or less at -26°C as measured according to ASTM D2983.

[0415] Embodiment 110. A lubricating fluid according to any one of Embodiments 103 to 109, wherein the lubricating fluid has a Brinell viscosity of 120,000 mPa·s or less at -26°C as measured according to ASTM D2983.

[0416] Embodiment 111. A lubricating fluid according to any one of Embodiments 103 to 110, wherein the lubricating fluid has a Brinell viscosity of 110,000 mPa·s or less at -26°C as measured according to ASTM D2983.

[0417] Embodiment 112. A lubricating fluid according to any one of Embodiments 103 to 111, wherein the lubricating fluid has a Brinell viscosity of 100,000 mPa·s or less at -26°C as measured according to ASTM D2983.

[0418] Embodiment 113. A lubricating fluid according to any one of Embodiments 103 to 112, wherein the lubricating fluid has a Brinell viscosity of 90,000 mPa·s or less at -26°C as measured according to ASTM D2983.

[0419] Embodiment 114. A lubricating fluid according to any one of Embodiments 103 to 113, wherein the lubricating fluid has a Brinell viscosity of 80,000 mPa·s or less at -26°C as measured according to ASTM D2983.

[0420] Embodiment 115. A lubricating fluid according to any one of Embodiments 103 to 114, wherein the lubricating fluid has a Brinell viscosity of 70,000 mPa·s to 100,000 mPa·s as measured according to ASTM D2983 at -26°C.

[0421] Example 116. The lubricating fluid according to Example 103, wherein the lubricating fluid has an MRV viscosity of 17,000 mPa·s or less as measured by ASTM D4684 at the test temperature.

[0422] Embodiment 117. A lubricating fluid according to any one of Embodiments 103 and 116, wherein the lubricating fluid has an MRV viscosity of 16,000 mPa·s or less as measured according to ASTM D4684 at the test temperature.

[0423] Embodiment 118. A lubricating fluid according to any one of Embodiments 103, 116 and 117, wherein the lubricating fluid has an MRV viscosity of 14,000 mPa·s to 15,000 mPa·s as measured according to ASTM D4684 at the test temperature.

[0424] Embodiment 119. A lubricating fluid according to any one of Embodiments 103 to 118, wherein the lubricating fluid has a pour point depressant additive content of 0.7% by weight or less.

[0425] Embodiment 120. A lubricating fluid according to any one of Embodiments 103 to 119, wherein the lubricating fluid has a pour point depressant additive content of 0.3% by weight or less.

[0426] Embodiment 121. A lubricating fluid according to any one of Embodiments 103 to 120, wherein the lubricating fluid has a polyalphaolefin content of 10% by weight or less.

[0427] Embodiment 122. A lubricating fluid according to any one of Embodiments 103 to 121, wherein the lubricating fluid has a polyalphaolefin content of 5% by weight or less.

[0428] Embodiment 123. A lubricating fluid according to any one of Embodiments 103 to 122, wherein the lubricating fluid has a polyalphaolefin content of 0.01% to 1% by weight.

[0429] Embodiment 124. A lubricating fluid according to any one of Embodiments 103 to 123, wherein the base oil has a viscosity index of 80 to 120.

[0430] Embodiment 125. A lubricating fluid according to any one of Embodiments 103 to 124, wherein the lubricating fluid has a viscosity index improver additive content of 5% by weight or less.

[0431] Embodiment 126. A lubricating fluid according to any one of Embodiments 103 to 125, wherein the lubricating fluid has a viscosity index improver additive content of 0.01% to 1% by weight.

[0432] Embodiment 127. A lubricating fluid according to any one of Embodiments 103 to 126, wherein the lubricating fluid has a viscosity index improver additive selected from: polyacrylate, polymers of methacrylate, polymers of butadiene, polymers of olefins, polymers of alkylated styrene, copolymers of methacrylate, copolymers of butadiene, copolymers of olefins, copolymers of alkylated styrene, copolymers of ethylene, copolymers of propylene, block copolymers of hydrogenated styrene, block copolymers of hydrogenated isoprene, and combinations thereof.

[0433] Embodiment 128. A lubricating fluid according to any one of Embodiments 103 to 127, wherein the lubricating fluid has a saturated compound content of at least 70% by weight.

[0434] Embodiment 129. A lubricating fluid according to any one of Embodiments 103 to 128, wherein the lubricating fluid has a saturated compound content of at least 80% by weight.

[0435] Embodiment 130. A lubricating fluid according to any one of Embodiments 103 to 129, wherein the lubricating fluid has an antioxidant additive content of 0.1% by weight or less.

[0436] Embodiment 131. A lubricating fluid according to any one of Embodiments 103 to 130, wherein the lubricating fluid has an antioxidant additive content of 0.01% to 0.05% by weight.

[0437] Embodiment 132. The lubricating fluid according to any one of Embodiments 103 to 131, wherein the lubricating fluid is automotive gear oil.

[0438] Embodiment 133. The lubricating fluid according to any one of Embodiments 103 to 131, wherein the lubricating fluid is engine oil.

[0439] Embodiment 134. The lubricating fluid according to any one of Embodiments 103 to 131, wherein the lubricating fluid is an industrial gear oil.

[0440] Implementation 135. A method of manufacturing an anti-deposit fluid, the method comprising: combining a base oil with one or more additives to form a blended fluid configured to resist the formation of deposits in an oxidizing environment; wherein the base oil has a viscosity index of at least 80 and a kinematic viscosity of at least 320 cSt at 40°C or at least 14 cSt at 100°C; and wherein the base oil comprises: greater than or equal to about 90% by weight of a saturated compound, less than or equal to about 10% by weight of an aromatic compound, and at least 1.7 terminal / side propyl groups and terminal / side ethyl groups per 100 carbon atoms.

[0441] Embodiment 136. The method according to Embodiment 135, wherein the blended fluid is configured to resist oxidation in the oxidizing environment, and the blended fluid is selected from: base oils, lubricants, process fluids, hydraulic fluids, industrial fluids, automotive fluids, and combinations thereof.

[0442] Embodiment 137. The method according to any one of Embodiments 135 and 136, wherein the oxidizing environment includes a temperature of up to 250℉ (121°C).

[0443] Embodiment 138. The method according to any one of Embodiments 135 to 137, wherein the oxidizing environment includes a temperature of up to 302℉ (150°C).

[0444] Embodiment 139. The method according to any one of Embodiments 135 to 138, wherein the oxidizing environment includes a temperature of up to 325℉ (163°C).

[0445] Embodiment 140. The method according to any one of Embodiments 135 to 139, wherein the oxidizing environment includes air.

[0446] Embodiment 141. The method according to any one of Embodiments 135 to 140, wherein the blended fluid is configured to resist the formation of deposits for at least 50 hours at temperatures up to 325℉ (163°C) in the presence of a metallic reagent.

[0447] Embodiment 142. The method according to any one of Embodiment 141, wherein the metal reagent is selected from copper, steel, iron, and combinations thereof.

[0448] Embodiment 143. The method according to any one of Embodiments 135 to 142, wherein the blended fluid is configured to resist the formation of deposits for at least 50 hours in the presence of water at temperatures up to 325℉ (163°C).

[0449] Embodiment 144. The method according to any one of Embodiments 135 to 143, wherein the blended fluid has an increase of 6% or less in kinematic viscosity (KV100) as measured according to ASTM D2893 at 100°C.

[0450] Embodiment 145. The method according to any one of Embodiments 135 to 144, wherein the blended fluid has an increase of 3% or less in kinematic viscosity (KV100) as measured according to ASTM D2893 at 100°C.

[0451] Embodiment 146. The method according to any one of Embodiments 135 to 145, wherein the blended fluid has an increase of 30% or less in kinematic viscosity (KV100) as measured according to ASTM D5704 at 100°C.

[0452] Embodiment 147. The method according to any one of Embodiments 135 to 146, wherein the blended fluid has an increase of 20% or less in kinematic viscosity (KV100) as measured according to ASTM D5704 at 100°C.

[0453] Embodiment 148. The method according to any one of Embodiments 135 to 147, wherein the blended fluid has an increase of 15% or less in kinematic viscosity (KV100) as measured according to ASTM D5704 at 100°C.

[0454] Embodiment 149. The method according to any one of Embodiments 135 to 148, wherein the blended fluid has an average carbon deposit / sludge grade of 8 to 10 as measured according to ASTM D5704.

[0455] Embodiment 150. The method according to any one of Embodiments 135 to 149, wherein the blended fluid has an average sludge grade of 8 to 10 as measured according to ASTM D5704.

[0456] Embodiment 151. The method according to any one of Embodiments 135 to 150, wherein the blended fluid has an average sludge grade of 9 to 10 as measured according to ASTM D5704.

[0457] Implementation 152. A method for maintaining or reducing deposit formation, the method comprising: introducing a base oil into a blended fluid; wherein: the base oil has a viscosity index of at least 80 and a kinematic viscosity of at least 320 cSt at 40°C or at least 14 cSt at 100°C; the base oil comprises: greater than or equal to about 90% by weight of a saturated compound, less than or equal to about 10% by weight of an aromatic compound, and at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms; and adding the base oil to the blended fluid maintains or enhances the ability of the blended fluid to resist deposit formation in an oxidizing environment.

[0458] Embodiment 153. The method according to Embodiment 152, wherein the blended fluid is configured to resist oxidation in the oxidizing environment, and the oxidizing environment includes a temperature of up to 250℉ (121°C).

[0459] Embodiment 154. The method according to any one of Embodiments 152 to 153, wherein the blended fluid is configured to resist oxidation in the oxidizing environment, and the oxidizing environment includes a temperature of up to 302℉ (150°C).

[0460] Embodiment 155. The method according to any one of Embodiments 152 to 154, wherein the blended fluid is configured to resist oxidation in the oxidizing environment, and the oxidizing environment includes a temperature of up to 325℉ (163°C).

[0461] Implementation 156. A method for mitigating deposit formation in a device, the method comprising: introducing a blended fluid into a metal component of the device; wherein: the blended fluid comprises a base oil and one or more additives; the base oil has a viscosity index of at least 80 and a kinematic viscosity of at least 320 cSt at 40°C or at least 14 cSt at 100°C; the base oil comprises: greater than or equal to about 90% by weight of a saturated compound, less than or equal to about 10% by weight of an aromatic compound, and at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms; and the blended fluid is configured to resist deposit formation in an oxidizing environment.

[0462] Embodiment 157. The method according to Embodiment 156, wherein the blended fluid is configured to resist oxidation in the oxidizing environment, and the blended fluid is selected from: base oils, lubricants, process fluids, hydraulic fluids, industrial fluids, automotive fluids, and combinations thereof.

[0463] Embodiment 158. The method according to any one of Embodiments 156 to 157, wherein the oxidizing environment includes a temperature of up to 250℉ (121°C).

[0464] Embodiment 159. The method according to any one of Embodiments 156 to 158, wherein the oxidizing environment includes a temperature of up to 302℉ (150°C).

[0465] Embodiment 160. The method according to any one of Embodiments 156 to 159, wherein the oxidizing environment includes a temperature of up to 325℉ (163°C).

[0466] Embodiment 161. The method according to any one of Embodiments 156 to 160, wherein the oxidizing environment comprises air.

[0467] Implementation 162. The method according to any one of Implementations 156 to 161, wherein the blended fluid is configured to resist the formation of deposits for at least 50 hours at temperatures up to 325℉ (163°C) in the presence of a metallic reagent.

[0468] Embodiment 163. The method according to any one of Embodiment 162, wherein the metallic reagent is selected from copper, steel, iron, and combinations thereof.

[0469] Implementation 164. The method according to any one of Implementations 156 to 163, wherein the blended fluid is configured to resist the formation of deposits for at least 50 hours in the presence of water at temperatures up to 325℉ (163°C).

[0470] Embodiment 165. The method according to any one of Embodiments 156 to 164, wherein the blended fluid has an increase of 6% or less in kinematic viscosity (KV100) as measured according to ASTM D2893 at 100°C.

[0471] Embodiment 166. The method according to any one of Embodiments 156 to 165, wherein the blended fluid has an increase of 3% or less in kinematic viscosity (KV100) as measured according to ASTM D2893 at 100°C.

[0472] Embodiment 167. The method according to any one of Embodiments 156 to 166, wherein the blended fluid has an increase of 30% or less in kinematic viscosity (KV100) as measured according to ASTM D5704 at 100°C.

[0473] Embodiment 168. The method according to any one of Embodiments 156 to 167, wherein the blended fluid has an increase of 20% or less in kinematic viscosity (KV100) as measured according to ASTM D5704 at 100°C.

[0474] Example 169. The method according to any one of Examples 156 to 168, wherein the blended fluid has an increase of 15% or less in kinematic viscosity (KV100) as measured according to ASTM D5704 at 100°C.

[0475] Embodiment 170. The method according to any one of Embodiments 156 to 169, wherein the blended fluid has an average carbon deposit / sludge grade of 8 to 10 as measured according to ASTM D5704.

[0476] Implementation 171. The method according to any one of Implementations 156 to 170, wherein the blended fluid has an average sludge grade of 8 to 10 as measured according to ASTM D5704.

[0477] Implementation 172. The method according to any one of Implementations 156 to 171, wherein the blended fluid has an average sludge grade of 9 to 10 as measured according to ASTM D5704.

[0478] Embodiment 173. The method according to any one of Embodiments 156 to 172, wherein the metal component includes a gear.

[0479] All values ​​in the specific embodiments and claims herein are modified with “about” or “approximately” and take into account experimental errors and variations expected by those skilled in the art.

[0480] When lower and upper limits are listed herein, a range from any lower limit to any upper limit can be expected. Although exemplary embodiments of the invention have been specifically described, it should be understood that various other variations will be apparent to those skilled in the art and readily achievable without departing from the spirit and scope of the invention. Therefore, it is not intended that the scope of the claims be limited to the examples and descriptions set forth herein, but rather that the claims be interpreted to include all features of novelty present in the invention that are patentable, including all features that a person skilled in the art to which this invention pertains would consider its equivalent.

[0481] Although the foregoing describes embodiments of the present invention, other and additional embodiments of the present invention may be conceived without departing from the basic scope of the present invention, the scope of which is determined by the claims.

Claims

1. A method for preparing a lubricating fluid, the method comprising: Group II base oils are blended with at least one other base oil to form a lubricating fluid. The Class II base oils have the following characteristics: At least a T10 distillation point of 482℃, Viscosity index ranging from 95 to 113. Kinematic viscosity ranging from 320 cSt to 550 cSt at 40°C. Kinematic viscosity ranging from 25 cSt to 32 cSt at 100°C 90% or more of saturated compounds, Aromatic compounds less than or equal to 10% by weight, and There are at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms. The at least one other base oil comprises a Class I base oil and one or more additives. The lubricating fluid described herein has a saturated compound content of at least 70% by weight and less than 90% by weight and an oxidation performance of 30% or less, represented by an increase in kinematic viscosity (KV100) at 100°C as measured according to ASTM D5704, or Oxidation properties represented by an increase of 6% or less in kinematic viscosity (KV100) at 100°C as measured according to ASTM D2893.

2. The method of claim 1, wherein the lubricating fluid has an oxidation performance represented by an increase of 20% or less in kinematic viscosity (KV100) at 100°C as measured according to ASTM D5704.

3. The method of claim 1, wherein the lubricating fluid has an oxidation performance of 3% or less, represented by an increase in kinematic viscosity (KV100) at 100°C as measured according to ASTM D2893.

4. The method of claim 1, wherein the lubricating fluid has a Brinell viscosity of 70,000 mPa·s or less at -12°C, as measured by ASTM D2983.

5. The method of claim 1, wherein the lubricating fluid has a Brinell viscosity of 30,000 mPa·s to 40,000 mPa·s as measured according to ASTM D2983 at -12°C.

6. The method of claim 1, wherein the lubricating fluid has a Brinell viscosity of 150,000 mPa·s or less as measured by ASTM D2983 at -26°C.

7. The method of claim 1, wherein the lubricating fluid has a pour point depressant additive content of 0.7% by weight or less.

8. The method of claim 1, wherein the lubricating fluid has a polyalphaolefin content of 10% by weight or less.

9. The method of claim 1, wherein the lubricating fluid is automotive gear oil.

10. The method of claim 1, wherein the lubricating fluid is engine oil.

11. The method of claim 1, wherein the lubricating fluid is industrial gear oil.

12. A method for preparing a lubricating fluid, the method comprising: Group II base oils are blended with at least one other base oil to form a lubricating fluid. The Class II base oils have the following characteristics: At least a T10 distillation point of 482℃, Viscosity index ranging from 95 to 113. Kinematic viscosity ranging from 320 cSt to 550 cSt at 40°C. Kinematic viscosity ranging from 25 cSt to 32 cSt at 100°C 90% or more of saturated compounds, Aromatic compounds less than or equal to 10% by weight, and There are at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups per 100 carbon atoms. The at least one other base oil comprises a Class I base oil and one or more additives. The lubricating fluid has a saturated compound content of at least 70% by weight and less than 90% by weight and has a Brinell viscosity as measured according to ASTM D2983: 70,000 mPa·s or less at -12°C or 150,000 mPa·s or less at -26°C. Alternatively, the lubricating fluid may have an MRV viscosity of 18,000 mPa·s or less, as measured according to ASTM D4684 at a test temperature of -20°C to -8°C.

13. A lubricating fluid, said lubricating fluid comprising: Group II base oils, Group I base oils, and one or more additives, wherein: The Group II base oils have a T10 distillation point of at least 482°C. Viscosity index ranging from 95 to 113. Kinematic viscosity ranging from 320 cSt to 550 cSt at 40°C. Kinematic viscosity ranging from 25 cSt to 32 cSt at 100°C 90% or more of saturated compounds, Aromatic compounds less than or equal to 10% by weight, and Each 100 carbon atoms contains at least 1.7 terminal / side-chain propyl groups and terminal / side-chain ethyl groups; and The lubricating fluid has a saturated compound content of at least 70% by weight and less than 90% by weight, and an oxidation performance of 30% or less, represented by an increase in kinematic viscosity (KV100) at 100°C as measured according to ASTM D5704. The oxidation performance is represented by an increase of 6% or less in the kinematic viscosity (KV100) at 100°C as measured according to ASTM D2893.

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