JP2015520286A - Lubricating oil composition comprising heavy Fischer-Tropsch derived and alkylated aromatic base oil - Google Patents

Abstract

A lubricating composition comprising an FT superheavy base oil and an alkylated aromatic blend stock, wherein the FT superheavy base oil has a kinematic viscosity at 100 ° C. in the range of 19-35 mm 2 / sec. Of a lubricating composition comprising blending an FT superheavy base oil that fails the “Clarification” criteria (ASTM-D4176) with an alkylated aromatic blend stock to provide a lubricating composition that passes the “Clarification” criteria. A manufacturing method is also disclosed. [Selection figure] None

Description

  The present invention relates to a lubricating composition comprising a Fischer-Tropsch superheavy base oil. In particular, but not exclusively, the present invention relates to a lubricating composition comprising a Fischer-Tropsch derived base oil having a waxy haze component but having a clear appearance.

Waxy hydrocarbon feed, such as those synthesized from gaseous components such as CO and H _2, in particular Fischer-Tropsch waxes, such waxy hydrogenating the feed dewaxing or hydroisomerization / contact ( And / or solvent) dewaxing thereby removing long chain n-paraffins and less branched paraffins and / or rearranging / isomerizing to lower pour and cloudy more branched isoparaffins. Thus, it is known in the art to be suitable for conversion / treatment into a lubricating base oil. Lubricating base oils produced by converting / processing waxy hydrocarbon feeds of the type synthesized from gaseous components (ie from Fischer-Tropsch feeds) are used in the present invention as Fischer-Tropsch derived base oils or simple Called FT base oil.

The viscosity of the FT base oil can vary considerably. They have a kinematic viscosity (VK100) at 100 ° C. according to ASTM-D445 of at least about 3 mm ² / sec (cSt), for example about 5 mm ² / sec, or about 7 mm ² / sec, or about 14 mm ² / sec. can do. FT residual base oil having a VK100 of at least 15 mm ² / sec is often referred to in the art as FT extra heavy base oil. Some FT superheavy base oils may further have a VK100 of at least 17 mm ² / sec, or at least 20 mm ² / sec or at least 25 mm ² / sec.

  It is known in the art to produce so-called Fischer-Tropsch residual (or tower bottom) derived lubricating base oil (hereinafter referred to as FT residual base oil). Such FT residual base oils are often FT superheavy base oils and are obtained from the residual (or bottom) fraction obtained from distillation of at least partially isomerized Fischer-Tropsch feed. The at least partially isomerized Fischer-Tropsch feed can itself be subjected to a process such as dewaxing prior to distillation. The residual base oil can be obtained directly from the residual fraction or indirectly by a process such as dewaxing. The residual base oil can be free of side stream products recovered from the distillate, ie either from the atmospheric fractionation column or the vacuum column. In WO-02 / 070627, WO-2009 / 088061, and WO-2005 / 047439, representative methods for producing Fischer-Tropsch derived residual base oil are described.

  FT superheavy base oils, especially FT residual superheavy base oils, find use in numerous lubricant applications due to their superior properties such as their beneficial viscosity properties and purity. However, such base oils may have an undesirable appearance in the form of a waxy haze at ambient temperature.

  Waxy haze can be estimated or measured in a number of ways. The presence of waxy haze can be measured, for example, according to ASTM-D4176-04 (determining whether the fuel or lubricant meets the “clarification” criteria). ASTM-D4176-04 is described for fuel, but it also works for base oils. The presence or degree of waxy haze can also be quantified as turbidity using nephelometric turbidity units (NTU) measured, for example, as described in US-2011 / 0083995.

  The waxy haze in the FT residual base oil, which can also adversely affect the filterability of the oil, is due to the presence of long carbon chain length paraffins that are not fully isomerized (or pyrolyzed).

  The content of long carbon chain long paraffins resulting from the waxy hydrocarbon feed is particularly high in the residual fraction from which the residual base oil is derived. Also, since the pour point and cloud point are relatively high due to the presence of long carbon chain length paraffins, the residual fraction is usually subjected to one or more contact and / or solvent dewaxing steps. Such a dewaxing step is very effective in reducing the pour point and cloud point in the resulting FT residual base oil, and under some conditions, particularly in combination with filtration, to reduce or eliminate haze. Could also be helpful.

WO-02 / 070627 WO-2009 / 080681 WO-2005 / 047439 US-2011 / 0083995

  However, there is still a need for an improved effective and efficient solution to reduce haze in FT base oils, particularly superheavy base oils and residual base oils.

  The object of the present invention is therefore to address the problem of waxy haze in FT base oils or to solve at least one other problem associated with the prior art.

  Here, it may be that removing the waxy haze in the FT superheavy base oil using a conventional catalytic dewaxing process may be inefficient or ineffective in the worst case. Recognized by the inventors. Particularly in FT residual superheavy base oils made from heavy waxy hydrocarbon feeds, there has been great difficulty in removing haze by dewaxing. Based on this recognition, the inventors have developed a new approach that addresses the problem of waxy haze in FT superheavy base oils.

From a first aspect, the present invention comprises an FT superheavy base oil and an alkylated aromatic blend stock, wherein the FT superheavy base oil has a kinematic viscosity at 100 ° C. in the range of 19-35 mm ² / sec. It exists in things.

  FT superheavy base oil and alkylated aromatic blend stock have been found to synergize to provide a lubricating composition having good lubricating properties and stability in that the formation of waxy haze is reduced. . Alkylated aromatic blend stocks have been found to solubilize waxy cloudy materials in FT superheavy base oils, such as FT residual superheavy base oils made from heavy waxy hydrocarbon feeds. . FT superheavy base oil greatly increases the lubricating properties of the composition.

  From a second aspect, the present invention includes a method of making a lubricating composition comprising blending an FT superheavy base oil and an alkylated aromatic blend stock.

  From a third aspect, the present invention resides in the use of an alkylated aromatic blend stock for the purpose of reducing waxy haze in an FT superheavy base oil or a precursor composition comprising an FT superheavy base oil. This use can include blending the alkylated aromatic blend stock with an FT superheavy base oil or precursor composition to form a lubricating composition.

  From a fourth aspect, the present invention provides a FT superheavy base oil or FT superheavy comprising blending an alkylated aromatic blend stock with an FT superheavy base oil or precursor composition to form a lubricating composition. A method for reducing waxy haze in a precursor composition comprising a base oil.

  From a fourth aspect, the present invention is directed to lubricating one or more of an engine, such as a compression ignition engine, an industrial machine such as a compressor, a hydraulic pump, an industrial turbine, or a gearbox, and a power transmission system. The use of a lubricating composition comprising an FT superheavy base oil and an alkylated aromatic blend stock.

  Further details and preferred features of the invention are set forth in the detailed description below.

  The term “comprising” is used herein interchangeably with the term “including” and is an open, non-limiting term. However, this term also encompasses "consisting of" and may always be limited to such provisions in some aspects of the invention where the context allows. In order to avoid misunderstandings, the preferred optional features of the invention can be applied to the respective forms of the invention where the context allows.

  The first essential component of the present invention is an FT superheavy base oil component. “FT superheavy base oil” is a Fischer-Tropsch derived hydrocarbon base oil product containing saturated paraffin molecules. Due to the superheavy oil, this usually tends to form a waxy haze. The FT superheavy base oil can be characterized by one or more of the features described herein below and has no further limiting technical meaning based on the name “superheavy”.

  The FT superheavy base oil may typically contain at least 95% by weight saturated hydrocarbon molecules. Preferably, the FT superheavy base oil is made from Fischer-Tropsch wax and contains greater than 98% by weight saturated hydrocarbons. Preferably, at least 85%, more preferably at least 90%, even more preferably at least 95%, and most preferably at least 98% by weight of these saturated hydrocarbon molecules are isoparaffinic. Preferably, at least 85% by weight of the saturated paraffinic hydrocarbon is an acyclic hydrocarbon. The naphthenic compound (paraffinic cyclic hydrocarbon) is preferably present in an amount of 15% by weight or less, more preferably less than 10% by weight.

  The FT superheavy base oil preferably contains hydrocarbon molecules having a continuous number of carbon atoms and has a continuous series of continuous isoparaffins, ie n, n + 1, n + 2, n + 3, and n + 4 carbon atoms. It contains isoparaffin. This series is the result of conducting a Fischer-Tropsch synthesis reaction, from which a superheavy base oil is derived, followed by isomerization of the wax feed. FT superheavy base oils are usually liquid at the temperature and pressure conditions used and usually but not always at standard atmospheric temperature and pressure.

We have determined that the degree of waxy cloudiness in FT superheavy base oil is high viscosity, high boiling point, high percentage of _{C30 +} molecules, high cloud point, high pour point, relatively low degree of isomerization, distillate. We have found that there is a tendency to increase with catalytic dewaxing as opposed to oil derivation from residual fractions rather than product, especially oils from heavy waxy hydrocarbon feeds, and solvent dewaxing. The persistence of cloudiness, particularly in connection with dewaxing, may also be associated with these factors. FT superheavy base oils that exhibit and / or persist the formation of waxy haze are particularly preferred as components that enjoy the benefits of the present invention and are therefore effective and economical to use in the present invention.

The kinematic viscosity at 100 ° C. (VK100) according to ASTM-D445 of FT superheavy base oil may usually be at least 15 mm ² / sec. Preferably, the VK100 is at least 17 mm ² / sec, more preferably at least 18 mm ² / s, even more preferably at least 19 mm ² / s, even more preferably at least 22 mm ² / s, even more preferably at least 24 mm ² / May be seconds. In some aspects, the VK 100 may be up to 100 mm ² / sec, or even up to 80 mm ² / sec, or up to 50 mm ² / sec, or even up to 35 mm ² / sec.

Alkylated aromatic kinematic viscosity (VK40) is at 40 ° C. according to blendstock ASTM-D445, a range of 20 mm ² / s to 300 mm ² / s as the case, the range preferably of 100 mm ² / sec ~250mm ² / sec It may be.

  The viscosity index of the FT superheavy base oil is preferably greater than 140 and preferably less than 170.

  The FT superheavy base oil may have a lower distillation temperature (T5 or 5% distillation) of at least 420 ° C. More preferably, the low distillation temperature (T5 or 5% distillation) may be at least 450 ° C, even more preferably at least 470 ° C. The high distillation temperature (T80 or 80% distillation) of the FT superheavy base oil may be at least 600 ° C. More preferably, the high distillation temperature (T80) may be at least 620 ° C, even more preferably at least 640 ° C. The low and high distillation temperature values referred to in the present invention are nominal values and refer to T5 and T80 distillation temperatures obtained by gas chromatographic simulation distillation (GCD) according to ASTM-D7169.

  In the present invention, the boiling range distribution of the sample is measured according to ASTM-D7169. Since Fischer-Tropsch derived hydrocarbons contain a mixture of components of various molecular weights having a wide boiling range, this disclosure refers to multiple boiling range recovery points. For example, a 10 wt% recovery point refers to a temperature at which 10 wt% of the hydrocarbons present in the fraction can be vaporized at atmospheric pressure and thus recovered. Similarly, the 90 wt% recovery point refers to the temperature at which 90 wt% of the hydrocarbons present vaporize at atmospheric pressure. Unless otherwise indicated, when referring to the boiling range distribution, this specification refers to a boiling range between 10 wt% recovered boiling point and 90 wt% recovered boiling point.

The FT superheavy base oil may preferably contain at least 95% by weight of _{C30 +} hydrocarbon molecules. More preferably, the FT _superheavy base oil may comprise at least 75% by weight _{C35 +} hydrocarbon molecules.

  “Cloud point” refers to the temperature at which a sample begins to cloud, as measured according to ASTM-D 5773. The FT superheavy base oil may have a cloud point in the range of + 60 ° C to + 5 ° C. Preferably, the FT superheavy base oil is in the range of + 50 ° C to + 10 ° C, more preferably in the range of + 45 ° C to + 15 ° C, more preferably in the range of + 40 ° C to + 20 ° C, most preferably in the range of + 31 ° C to + 20 ° C. With a cloud point of

  “Pour point” refers to the temperature at which a sample begins to flow under carefully controlled conditions. The pour point referred to in this specification was determined according to ASTM-D97-93. FT superheavy base oil is -9 ° C or lower, preferably -12 ° C or -15 ° C or -21 ° C or -24 ° C or -27 ° C or even -30 ° C or -36 ° C or -39 ° C or -45. It may have a pour point of ℃ or less. Thus, this may be a base oil of the type that has been subjected to relatively severe (ie hot contact) dewaxing that can provide a pour point of -30 ° C or lower, eg, -30 to -45 ° C. Such base oils may still contain residual waxy haze and can thus benefit from the present invention. Alternatively, the FT superheavy base oil may have been subjected to a relatively mild dewaxing that provides a pour point higher than −30 ° C., for example at least −15 ° C., for example in the range of −12 ° C. to 0 ° C.

  FT superheavy base oil can be further characterized by its different carbon species content. More particularly, the FT superheavy base oil is a repetitive methylene that is more than 4 carbons away from the nearest end group and the nearest branch compared to its ε-methylene carbon atom proportion, ie its isopropyl carbon atom proportion. It can be characterized by the proportion of carbon (further referred to as CH2> 4). In the following specification, the ratio of the proportion of ε-methylene carbon atoms to the proportion of isopropyl carbon atoms (ie carbon atoms in the isopropyl branch) as measured for the entire base oil is referred to as the epsilon: isopropyl ratio. The isomerized FT residual base oil disclosed in U.S. Pat. No. 7,053,254 is less than 8.2% of the latter compound relative to the Fischer-Tropsch derived paraffinic base oil component obtained at higher dewaxing severity. It has been found that the epsilon: isopropyl ratio is different. Both these types of FT superheavy base oils are useful in the present invention. Mildly dewaxed superheavy base oils having an isopropyl ratio higher than 8.2 can often contain a more pronounced waxy haze. However, it has been found that severely dewaxed superheavy base oils having an epsilon: isopropyl ratio of 8.2 or less can also have residual haze and thus surprisingly can enjoy the benefits of the present invention. It was done.

  The branching in the FT superheavy base oil can also be expressed as the average degree of branching. Such average degree of branching of FT superheavy base oils, in some embodiments, ranged from 6.5 to about 10 alkyl branches per 100 carbon atoms as disclosed in US-7,053,254. It's okay. In other embodiments, the average degree of branching in the molecule may be greater than 10 alkyl branches per 100 carbon atoms as measured in accordance with the method disclosed in US-A-70553254.

The branching properties and carbon composition of the Fischer-Tropsch derived base oil blend components are described in ¹³ C-NMR, vapor pressure osmometry (VPO), and field ionization mass spectrometry, as described in US-8,152,869. It can be easily determined by analyzing a sample of oil using (FIMS).

  The FT superheavy base oil may have a viscosity index (ASTM-D2270) usually between 120 and 180. This preferably contains no or very little sulfur and nitrogen containing compounds. This is normal for products derived from Fischer-Tropsch reactions using synthesis gas that is substantially free of heteroatom impurities. Preferably, the FT superheavy base oil contains sulfur, nitrogen, and metals in the form of hydrocarbon compounds containing them in an amount of less than 50 ppmw (weight ppm), more preferably less than 20 ppmw, even more preferably less than 10 ppmw. Including. Most preferably, sulfur and nitrogen are included, generally at a level below the detection limit, which is 5 ppmw for sulfur and 1 ppmw for nitrogen when using, for example, X-ray or “Antek” nitrogen tests for measurement. It is.

  The FT superheavy base oil is preferably FT residual base oil, i.e., obtained from a residual or high vacuum tower bottom fraction from hydrocarbons produced during the Fischer-Tropsch synthesis reaction.

  More preferably, this fraction is a distillation residue containing the highest molecular weight compounds still present in the product after the hydroisomerization step. The 10 wt% recovery boiling point of such fractions is preferably higher than 370 ° C, more preferably higher than 400 ° C, and most preferably higher than 480 ° C for some embodiments of the present invention.

The density of the FT superheavy base oil component as measured by standard test method IP-365 / 97 is suitably about 700-1100 kg / m ³ , preferably about 834-841 kg / m ³ .

  In its broadest sense, the present invention encompasses the use of a paraffinic heavy base oil having one or more of the properties described above, regardless of whether the component is Fischer-Tropsch derived. The FT superheavy base oil component may comprise a mixture of two or more FT superheavy base oils.

  To produce an FT superheavy base oil for use in the present invention, the Fischer-Tropsch derived residual fraction or bottom product is preferably subjected to an isomerization process. This converts n-paraffins to isoparaffins, thus increasing the degree of branching in the hydrocarbon molecules and improving the low temperature flow characteristics. Depending on the catalyst and isomerization conditions used, long chain hydrocarbon molecules having relatively highly branched end regions can be obtained. Such molecules tend to exhibit relatively good cold flow performance. The isomerized bottom product can be subjected to further downstream processes such as hydrocracking, hydrotreating, and / or hydrofinishing. This is preferably subjected to a dewaxing step by solvent dewaxing or more preferably by catalytic dewaxing as described below, which further serves to lower its pour point. However, even after dewaxing, the FT residual superheavy base oil still has residual waxy haze due to ultra high molecular weight molecules that cannot be completely removed by the dewaxing process.

  In general, FT superheavy base oils for use in the present invention can be produced by any suitable Fischer-Tropsch process. Preferably, however, the FT superheavy base oil component (b) hydrogenates a Fischer-Tropsch derived feed, in which (a) at least 20% by weight of the compounds in the Fischer-Tropsch derived feed has at least 30 carbon atoms. Cracking / hydroisomerization; (b) separating the product of step (a) into one or more distillation fractions and preferably a heavy residue fraction containing at least 10% by weight of compounds with a boiling point above 540 ° C .; (C) subjecting the residual fraction to a catalytic pour point reduction step; and (d) isolating the Fischer-Tropsch derived paraffinic heavy base oil component from the effluent of step (c), preferably as the residual heavy fraction. Obtained from a Fischer-Tropsch derived wax or waxy raffinate feed stream It is the quality bottoms fraction.

  In addition to isomerization and fractionation, the Fischer-Tropsch derived product fraction can be subjected to various other operations such as hydrocracking, hydrotreating, and / or hydrofinishing.

  The feed stream from step (a) is a Fischer-Tropsch derived product. The initial boiling point of the Fischer-Tropsch product may be 400 ° C. or less. Preferably, compounds having 4 or fewer carbon atoms and compounds having boiling points in this range are separated from the Fischer-Tropsch synthesis product before the Fischer-Tropsch synthesis product is used in such a hydroisomerization step.

  Examples of suitable Fischer-Tropsch processes are described in WO-A-99 / 34917 and AU-A-698391. The disclosed process provides the Fischer-Tropsch product described above. Fischer-Tropsch products can be obtained by well-known processes such as the so-called Sasol process, Shell middle distillate synthesis process, or ExxonMobil “AGC-21” process. These and other processes can be found in, for example, EP-A-0776959, EP-A-0666842, US-A-4493672, US-A-5059299, WO-A-99 / 34917, and WO-A-99 / 20720. It is described in detail. The Fischer-Tropsch process generally includes Fischer-Tropsch synthesis and hydroisomerization steps, as described in these publications. Fischer-Tropsch synthesis can be performed on any type of hydrocarbonaceous material such as coal, natural gas, or syngas produced from biological materials such as wood or hay.

  Fischer-Tropsch products obtained directly from the Fischer-Tropsch process usually contain a waxy fraction that is solid at room temperature.

The feed to the hydroisomerization step (a) preferably comprises at least 30% by weight, preferably at least 50% by weight, more preferably at least 55% by weight of the compound having at least 30 carbon atoms. Tropsch product. Furthermore, the weight ratio of the compound having at least 60 carbon atoms to the compound having at least 30 but less than 60 carbon atoms in the feed is preferably at least 0.2, more preferably at least about 0.1. 4, most preferably at least 0.55. If the feed has a 10 wt% recovery boiling point above 500 ° C, the wax content is preferably greater than 50 wt%. Preferably, the Fischer-Tropsch product has an ASF-α value (Anderson-Schulz-Flory linkage) of at least 0.925, preferably at least 0.935, more preferably at least 0.945, even more preferably at least 0.955. C ₂₀₊ fraction having a growth factor).

  The hydrocracking / hydroisomerization reaction of step (a) is preferably carried out in the presence of hydrogen and a catalyst, the catalyst being selected from those known to those skilled in the art to be suitable for this reaction. Can do. Catalysts for use in hydroisomerization usually have an acidic functional component and a hydrogenation-dehydrogenation functional component. A preferred acidic functional component is a refractory metal oxide support. Suitable carrier materials include silica, alumina, silica-alumina, zirconia, titania, and mixtures thereof. Preferred support materials for inclusion in the catalyst are silica, alumina, and silica-alumina. A particularly preferred catalyst comprises platinum supported on a silica-alumina support. Preferably, the catalyst does not contain a halogen compound such as fluorine. This is because the use of such a catalyst may require special operating conditions and may involve environmental problems. Examples of suitable hydrocracking / hydroisomerization processes and catalysts are described in WO-A-00 / 14179, EP-A-0532118, EP-A-0666694, and EP-A-0776959.

  Preferred hydrogenation-dehydrogenation functional components are Group VIII metals such as cobalt, nickel, palladium, and platinum, more preferably platinum. In the case of platinum and palladium, the catalyst may contain a hydrogenation-dehydrogenation active component in an amount of 0.005 to 5 parts by weight, preferably 0.02 to 2 parts by weight per 100 parts by weight of the support material. it can. When nickel is used, a higher content is usually present, and in some cases nickel is used in combination with copper. Particularly preferred catalysts for use in the hydroconversion stage comprise platinum in an amount ranging from 0.05 to 2 parts by weight, more preferably from 0.1 to 1 part by weight per 100 parts by weight of the support material. The catalyst can also include a binder to increase the strength of the catalyst. The binder may be non-acidic. Examples are clay and other binders known to those skilled in the art.

  In hydroisomerization, the feed is contacted with hydrogen in the presence of a catalyst at elevated temperature and pressure. The temperature is usually in the range of 175 to 380 ° C, preferably higher than 250 ° C, more preferably 300 to 370 ° C. The pressure is usually in the range of 10 to 250 bar, preferably 20 to 80 bar. Hydrogen can be supplied at a gas hourly space velocity of 100-10000 NL / L / hour, preferably 500-5000 NL / L / hour. The hydrocarbon feed can be fed at a space hourly space velocity of 0.1-5 kg / L / hour, preferably higher than 0.5 kg / L / hour, more preferably lower than 2 kg / L / hour. The ratio of hydrogen to hydrocarbon feed may range from 100 to 5000 NL / kg, and is preferably from 250 to 2500 NL / kg.

  The conversion in hydroisomerization, defined as the weight percent of feeds with a boiling point higher than 370 ° C. reacting per pass to the fraction with a boiling point below 370 ° C., is preferably at least 20% by weight, preferably at least Although it is 25 weight%, Preferably it is 80 weight% or less, More preferably, it is 70 weight% or less. The feed used above in this definition is the total hydrocarbon feed that is fed to the hydroisomerization process and thus includes any optional recycle material to step (a).

  The resulting product of the hydroisomerization process preferably comprises at least 50% by weight, more preferably at least 60% by weight, and even more preferably at least 70% by weight isoparaffin, the rest being n-paraffin naphthenic compounds and aromatics. Consists of group compounds.

  In step (b), the product of step (a) is separated into one or more distillate fractions and preferably a residual heavy fraction containing at least 10% by weight of compounds with a boiling point above 540 ° C. This advantageously involves performing one or more distillate separations on the hydroisomerization process effluent to obtain at least one middle distillate fuel fraction and a residual fraction for use in step (c). Is done by.

  Preferably, the effluent from step (a) is first subjected to atmospheric distillation. The 10% by weight recovery boiling point of the residue may preferably be in the range of 350-550 ° C. This atmospheric tower bottom product or residue preferably boils at a temperature of at least 95% by weight above 370 ° C. The residue obtained in such distillation can be subjected to further distillation, which in some preferred embodiments is carried out at near vacuum conditions, to reach a fraction having a higher 10% by weight recovery boiling point.

  This fraction can be used directly in step (c) or can be subjected to further vacuum distillation, preferably carried out at a pressure between 0.001 and 0.1 bar. The feed to step (c) is preferably obtained as the bottom product of such vacuum distillation.

  In step (c), the heavy residual fraction obtained in step (b) is subjected to a catalytic pour point lowering step. Step (c) can be carried out using any hydroconversion process that can reduce the wax content to a value lower than 50% by weight of its original value. The wax content in the intermediate product is preferably below 35% by weight, more preferably between 5 and 35% by weight, even more preferably between 10 and 35% by weight. The product obtained in step (c) preferably has a freezing point lower than 80 ° C. Preferably, more than 50%, more preferably more than 70% by weight of the intermediate product boils at a temperature above the 10% recovery point of the wax feed used in step (a).

  The wax content can be measured according to the following procedure. One part by weight of the oil fraction subjected to analysis is diluted with 4 parts of a mixture of methyl ethyl ketone and toluene (50/50 vol / vol), which is then cooled in a refrigerator to -20 ° C. The mixture is then filtered at -20 ° C. Wash the wax thoroughly with cold solvent, remove from the filter, dry and weigh. When referring to the oil content, the weight% value means a value obtained by subtracting the wax content (wt%) from 100 wt%.

  A possible process for step (c) is the hydroisomerization process described above for step (a). It has been found that such catalysts can be used to reduce the wax level to the desired level. By varying the severity of the process conditions as described above, one skilled in the art will readily determine the operating conditions necessary to reach the desired wax conversion. However, in order to optimize the oil yield, a temperature between 300 and 330 ° C. and between 0.1 and 5 kg of oil per hour per liter of catalyst (kg / L / hr), More preferably, a weight hourly space velocity between 0.1 and 3 is particularly preferred. A more preferred class of catalyst that can be applied in step (c) is the class of dewaxing catalyst. The process conditions applied when using such a catalyst must be such that the wax content remains in the oil. In contrast, conventional catalytic dewaxing processes aim to reduce the wax content to nearly zero. When a dewaxing catalyst containing molecular sieves is used, more heavy molecules remain in the dewaxed oil. Thereafter, a more viscous base oil can be obtained.

  The dewaxing catalyst that can be applied in step (c) preferably comprises a molecular sieve, optionally in combination with a metal having a hydrogenating function, such as a Group VIII metal. Molecular sieves, more preferably molecular sieves having a pore size between 0.35 and 0.8 nm, showed good catalytic ability to reduce the wax content of the wax feed. Suitable zeolites are mordenite, beta, ZSM-5, ZSM-12, ZSM-22, ZSM-23, SSZ-32, ZSM-35, ZSM-48, EU-2, and combinations of such zeolites. Of these, ZSM-12, ZSM-48, and EU-2 are most preferred.

In the present invention, references to ZSM-48 and EU-2 are also referred to as ^* MREs and are described in “Catalog of Disorder in Zeolite Frameworks” published in 2000 on behalf of the International Zeolite Association Structural Committee. It is used to show that all zeolites belonging to the irregularly structured ZSM-48 class can be used. Even though EU-2 is considered different from ZSM-48, both ZSM-48 and EU-2 can be used in the present invention. The zeolites ZBM-30 and EU-11 are very similar to ZSM-48, and these are also considered to be a kind of zeolite belonging to the ZSM-48 class. In this application, reference to ZSM-48 zeolite also refers to ZBM-30 and EU-11 zeolite. In addition to ZSM-48 and / or EU-2 zeolite, additional zeolites can be present in the catalyst composition, particularly if it is desired to modify its catalytic properties. It has been found that it may be advantageous to give ZSM-12, the zeolite specified in the "Database of Zeolite Structure" published in 2007/2008 on commission of the International Zeolite Society's Structural Committee It was done.

  Another preferred group of molecular sieves are silica-alumina phosphate (SAPO) materials, of which SAPO-11, for example as described in US-A-4859311, is most preferred. In some cases, ZSM-5 can be used in its HZSM-5 form in which no Group VIII metal is present. Other molecular sieves are preferably used in combination with the added Group VIII metal. Preferred Group VIII metals are nickel, cobalt, platinum, and palladium. Examples of possible combinations are Pt / ZSM-35, Ni / ZSM-5, Pt / ZSM-23, Pd / ZSM-23, Pt / ZSM-48, and Pt / SAPO-11, or Pt / zeolite beta A laminated structure of Pt / ZSM-23, Pt / zeolite beta and Pt / ZSM-48, or Pt / zeolite beta and Pt / ZSM-22. Further details and examples of suitable molecular sieves and dewaxing conditions can be found, for example, in WO-A-97 / 18278, US-A-4434369, US-A-5053373, US-A-5252527, US-A-2004 / 0065581. , US-A-45744033, and EP-A-1029029. Other preferred types of molecular sieves include those with relatively low isomerization selectivity and high wax conversion selectivity, such as ZSM-5 and ferrierite (ZSM-35).

  The dewaxing catalyst preferably also includes a binder. The binder may be a synthetic or natural (inorganic) material such as clay, silica, and / or metal oxide. Natural clays are, for example, those of montmorillonite and kaolins. The binder is preferably a porous binder material, such as a refractory oxide, examples of which include alumina, silica-alumina, silica-magnesia, silica-zirconia, silica-tria, silica-beryllia, and silica-titania, And ternary compositions such as silica-alumina-tria, silica-alumina-zirconia, silica-alumina-magnesia, and silica-magnesia-zirconia. More preferably, a low acidity heat-resistant oxide binder material substantially free of alumina is used. Examples of these binder materials are silica, zirconia, titanium dioxide, germanium dioxide, boria, and mixtures of two or more thereof, examples of which are given above. The most preferred binder is silica. The second preferred binder is titania.

  A preferred type of dewaxing catalyst comprises the above intermediate zeolite microcrystals and the low acidity heat-resistant oxide binder material substantially free of alumina, and the surface of the aluminosilicate zeolite microcrystals is aluminosilicate zeolite It has been modified by subjecting the microcrystals to a surface dealumination treatment. A preferred dealumination treatment involves contacting the binder and zeolite extrudates with an aqueous solution of a fluorosilicate salt as described, for example, in US-A-5157191 or WO-A-00 / 29511. Examples of suitable dewaxing catalysts mentioned above are, for example, silica-bonded dealuminated Pt / ZSM-5 or silica-bonded dealuminated Pt / ZSM-35 as described in WO-A-00 / 29511 and EP-B-083171. It is.

  The conditions in step (c) when using a dewaxing catalyst usually include an operating temperature in the range of 200-500 ° C, preferably 250-400 ° C. Preferably, the temperature is between 300-330 ° C. The hydrogen pressure may range from 10 to 200 bar, preferably from 40 to 70 bar. The weight hourly space velocity (WHSV) is 0.1 to 10 kg / L / hour, preferably 0.1 to 5 kg / L / hour, in terms of kg of oil per hour (kg / L / hour) per liter of catalyst. More preferably, it may be in the range of 0.1 to 3 kg / L / hour. The ratio of hydrogen to oil may range from 100 to 2000 L of hydrogen per liter of oil.

  In step (d), the product of step (c) is usually sent to a vacuum column where various distillate base oil fractions are recovered. These distillate base oil fractions can be used to produce lubricating base oil blends, or they can be broken down into lower boiling products such as diesel or naphtha. The residual material recovered from the vacuum column contains a mixture of high-boiling hydrocarbons, which can be used to produce an FT superheavy base oil for use in the present invention.

  Furthermore, the product obtained in step (c) can also be used to remove unwanted components, for example in a clay treatment process, for example as described in US Pat. No. 4,795,546 and EP-A-0712922, or Further processing can be achieved by contacting with activated carbon. Other processes suitable for producing heavy and ultraheavy Fischer-Tropsch derived base oils are described in WO-A-2004 / 033607, US-A-70553254, EP-A-1366134, EP-A-1382639, EP -A-1516038, EP-A-1534801, WO-A-2004 / 003113, and WO-A-2005 / 063941.

  FT superheavy base oil is defined and described as an additive component in the present invention. This may in some cases represent the sole source of FT superheavy base oil in the lubricating composition, but this is not essential. Thus, other FT superheavy base oils can be present in the lubricating composition and the amount of FT superheavy base oil indicated in the present invention should be interpreted accordingly unless otherwise required by context. I must.

  The FT superheavy base oil can be composed of, or can be synonymous with, any FT superheavy base oil described or defined herein, or any combination thereof.

  FT superheavy base oil fails the “Clarification” criteria (ASTM-D4176-04) at standard conditions and / or is at least 0.5 NTU (turbidimetric turbidity unit), preferably at least 1 NTU, more preferably May tend to form haze in the sense of having a measurable turbidity of at least 2 NTU, even more preferably at least 3 NTU, most preferably at least 4 NTU. Turbidity can be measured at 25 ° C. according to the method described in US2011 / 0083995. The FT superheavy base oil may be hazy.

  The amount of FT superheavy base oil can be adjusted to achieve the desired waxy haze reduction and viscosity performance. The effective amount of FT superheavy base oil is determined in part by the nature of the FT superheavy base oil and the nature of the alkylated aromatic blend stock combined therewith.

  In some aspects of the invention, the amount of FT superheavy base oil is 5-50% by weight, preferably 10-40% by weight, based on the combined weight of the FT superheavy base oil and the alkylated aromatic blend stock. More preferably, it is 15 to 35% by weight, particularly 20 to 25% by weight.

  The second essential component of the present invention is an alkylated aromatic blend stock. The alkylated aromatic blend stock may contain or consist of one or more alkylated aromatic compounds (alkylated aromatics) that are consistent with achieving the desired properties in the lubricating composition. it can.

  The alkylated aromatic material has an aromatic head group and at least one alkyl chain.

  The aromatic head group may be a substituted or unsubstituted monocyclic or polycyclic structure. Aromatic head groups containing one or more heteroatoms may also be suitable. Preferred aromatic head groups in the context of the present invention are benzene and naphthalene, with naphthalene being particularly preferred.

Preferably, one or more alkyl chains of alkylated aromatics _are each independently a linear alkyl group of C 1 _{-C 30,} for example _C 1 _{-C 20;} or _C 3 _{-C 300,} for example _C 3 -C _100, or _C 3 branched alkyl group having _{-C 30;} may be. Longer alkyl chains can help reduce volatility and improve viscosity properties. In some embodiments of the present invention, the at least one linear or branched alkyl group of the alkylated aromatic material preferably contains at least 10 carbon atoms, more preferably at least 15 carbon atoms. Well, for example, C ₁₀ -C ₃₀ or C ₁₀ -C ₂₀ or C ₁₅ -C ₃₀ or C ₁₀ -C ₁₅ linear alkyl groups, or C ₁₀ -C ₃₀₀ or C ₁₀ -C ₁₀₀ , or C ₁₀ -C _It may be ₃₀ or a C ₁₅ -C ₃₀₀ or C ₁₅ -C ₁₀₀ , or C ₁₅ -C ₃₀ branched alkyl group.

  The number of alkyl chains per aromatic head group may vary. One or more alkyl chains, such as one, two, three, four, five, or six alkyl chains may be directly attached to the aromatic system of the aromatic head group. The alkyl chain may be attached to the aromatic system at all available positions on the aromatic head group.

  In order to achieve the desired volatility properties, the average number of carbon atoms in the alkylated aromatic material may be at least 11, preferably at least 15, more preferably at least 25, or even at least 40. The alkylated aromatic material may have a number average molecular weight of at least about 150, preferably at least about 180, more preferably at least about 300, or even at least about 480.

The production of alkylated aromatics is well known in the art. Although any manufacturing method is suitable in the context of the present invention, suitable alkylated aromatic materials can conveniently be formed by an alkylation reaction between an aromatic compound and an alkylating agent. Olefin is a particularly common alkylating agent used in the art. The alkylation reaction is generally carried out on an acidic catalyst, in particular a Friedel-Crafts catalyst such as AlCl ₃ , BF ₃ , FeCl ₃ , acidic zeolite, amorphous aluminosilicate, acid clay, or acidic metal oxide. The alkylated aromatic material obtained by alkylation generally includes a mixture of compounds and isomers.

  As will be apparent to those skilled in the art, it is also possible to obtain short chain alkylated aromatics from refining or other petrochemical processes. Conveniently, such alkylated aromatic-containing feeds can be made from a suitable stream of aromatization obtained from the FT process. The alkylated aromatics obtained in this way can be used directly in the present invention or as alkylation feeds depending on the desired properties.

  Hydrogenated or partially hydrogenated analogs of the alkylated aromatics described herein may optionally be used in the alkylated aromatic blend stock or as the alkylated aromatic blend stock.

  Alkylated naphthalenes are particularly preferred alkylated aromatic materials for use in or as alkylated aromatic blend stocks. Alkylated naphthalenes useful in the context of the present invention are represented by the following general formula (I):

(Wherein, A + B = 1 to 8, preferably 1 to 6, more preferably 1 to 5, R _is, C 1 _{-C 30,} preferably linear alkyl group of _C 1 _{~C 20, C} 3 ~ C ₃₀₀ , preferably C ₃ -C ₁₀₀ , more preferably C ₃ -C ₃₀ branched alkyl groups, or a mixture of such groups, and the total number of carbons in R _A and R _B is preferably at least 4 Is)
You may have.

Representative examples of alkyl naphthalenes are the mono -, di -, tri -, tetra -, or penta -C ₃ alkyl naphthalenes, -C ₄ alkyl naphthalenes, -C ₅ alkyl naphthalenes, -C ₆ alkyl naphthalenes, -C ₈ alkylated naphthalenes, _{-C 10} alkyl naphthalenes, _{-C 12} alkyl naphthalenes, _{-C 14} alkyl naphthalenes, _{-C 16} alkyl naphthalenes, _{-C 18} alkyl _naphthalene, C 10 _{-C 14} mixed alkyl _{naphthalenes,} C 6 -C ₈ mixed alkylnaphthalenes, or mono -, di -, tri -, tetra -, or penta _{-C 3, C 4, C 5} , C 6, C 8, C 10, C 12, C 14, C 16, C 18, Or alkyl monomethyl, dimethyl, ethyl, diethyl, or methyl ethyl naphthalene in a mixed form thereof, or The mixtures thereof. Alkyl group or branched alkyl group, for example _C 10 _{-C 300,} for example, _C 24 _{-C 56} branched alkyl _{naphthalenes,} C 24 _{-C 56} branched alkyl mono -, di -, tri -, tetra - or penta _-C 1 ~ C ₄ naphthalene may also be used. These branched alkyl group-substituted naphthalenes, or branched alkyl group-substituted mono-, di-, tri-, tetra-, or penta-C ₁ -C ₄ naphthalenes can also be used as a mixture with the substances shown above. . If the branched alkyl group is very large (i.e., 8 to 300 carbons), usually only one or two of such alkyl groups are attached to the naphthalene head group. The alkyl group on the naphthalene ring may be a mixed form of any of the above plurality of alkyl groups.

  Usually alkyl naphthalenes are alkylated with naphthalene or short chain alkyl naphthalenes such as methyl or dimethyl naphthalene with olefins, alcohols or alkyl chlorides over acidic catalysts such as conventional Friedel-Crafts catalysts. Manufactured by. Methods for producing alkyl naphthalenes suitable for use in the present invention are cited in US-5,034,563, US-5,516,954, and US-6,436,882, and these patents. References, and other places in the literature. Since alkylated naphthalene synthesis techniques are well known in the art, such techniques are not further described herein.

  Suitable alkylated naphthalenes are commercially available from ExxonMobil Chemical Company® under the trade name Synesstic AN®.

  Alkylated benzenes are also preferred alkylated aromatics for use in the present invention. Alkylated benzenes useful in the context of the present invention have the general formula:

You may have. In this structure, C = 1 to 6, preferably 1 to 5, and more preferably 1 to 4. If this is the monoalkylated benzene, R represents a linear _C 10 _{-C 30} alkyl group, or a _C 10 _{-C 300} branched alkyl group, preferably a _C 10 _{-C 100} branched alkyl groups, more preferably _{C 15} ~C may be ₅₀ branched alkyl group. If C is greater than 2 or 2, C-1 or less alkyl groups, _{individually,} a small alkyl group having C 1 -C _5, preferably it is a _C 1 -C ₂ alkyl group, at least 1 One of the remaining alkyl groups are linear _C 10 _{-C 30} alkyl group, or a _C 10 _{-C 300} branched alkyl group, preferably a _C 10 _{-C 100} branched alkyl groups, more preferably _C 15 _{-C 50} branched alkyl group is there. Large branched alkyl group may be prepared from the oligomerization or polymerization of C ₃ -C ₂₀ internal or α- olefin or a plurality of mixtures of these olefins.

  Alkylated benzenes are produced by alkylating benzene or short-chain alkylbenzenes such as methyl or dimethylbenzene with olefins, alcohols, or alkyl chlorides over acidic catalysts such as conventional Friedel-Crafts catalysts. can do. Preferred alkylated benzene fluids can be prepared according to US-6,071,864 or US-6,491,809 or EP-0,168,534.

  The alkylated aromatic blend stock is defined and described as an additive component in the present invention. This may in some cases represent the sole source of alkylated aromatics in the lubricating composition, but this is not essential. Thus, other alkylated aromatics can be present in the lubricating composition and the amount of alkylated aromatic shown in the present invention should be construed accordingly unless otherwise required by context. I must.

  The alkylated aromatic blend stock can be composed of any alkylated aromatic material described or defined herein, or any combination thereof, such as alkylated naphthalenes and / or alkylated benzenes, or It may be synonymous with this.

Kinematic viscosity (VK 100) at 100 ° C. according to ASTM-D445 of alkylated aromatics blendstock, 1 mm ² / s ~50mm ² / s, preferably in the range 2 mm ² / sec ~30mm ² / sec range, more preferably is 3 mm ² / s to 20 mm ² / s range, and most preferably 4 mm ² / sec ~15mm ² / s, may be in the range of, for example, 4 to 7 mm ² / s or 11-15 mm ² / s.

Kinematic viscosity (VK40) at 40 ° C. according to ASTM-D445 of alkylated aromatics blendstock, 20 mm ² / sec ~150mm ² / s range, preferably a range of 25 mm ² / sec ~120mm ² / sec Good.

  The alkylated aromatic blend stock preferably has a pour point (ASTM-D97) of 0 ° C. or less, preferably −20 ° C., more preferably −30 ° C. or less; and / or about 0-200, preferably about 60- 200, more preferably about 70 to about 160, such as a viscosity index (ASTM-D2270) in the range of about 75 to about 110; and / or 15%, preferably 7%, more preferably less than 5% Noack Volatility (ASTM-D5800).

  The amount of alkylated aromatic blend stock can be adjusted to achieve the desired waxy haze reduction. The effective amount of alkylated aromatic blend stock is determined in part by the nature of the blend stock and the nature of the FT residual oil combined therewith.

  In some aspects of the invention, the amount of alkylated aromatic blend stock is 50-95 wt%, preferably 60-90 wt%, based on the combined weight of FT superheavy base oil and alkylated aromatic blendstock. %, More preferably 65 to 85% by weight, especially 75 to 80% by weight.

  The lubricating composition has a lower haze appearance than the FT superheavy base oil used to formulate it. Advantageously, the lubricating composition can pass the “clarification” criteria (ASTM-D4176-04). This is preferably at most 2 NTU, preferably at most 1 NTU, more preferably at most 0.5 NTU, even more preferably at most 0.2 NTU, measured at 25 ° C. according to the method of US-2011 / 0083995, ideal Specifically, it can have a turbidity of 0 NTU. Advantageously, the lubricating composition can meet one or more of the above haze measurements at least 14 days after blending.

Kinematic viscosity at 100 ° C. according to ASTM-D445 of the lubricating composition (VK 100) is preferably, 1 mm ² / s ~30mm ² / s, preferably in the range 2 mm ² / s 25 mm ² / s range, and more preferably can range it is of 3 mm ² / s to 20 mm ² / s range, and most preferably 4 mm ² / sec ~18mm ² / sec, for example, 7 to 12 mm ² / s or 14~17mm ² / sec.

Kinematic viscosity at 40 ° C. according to ASTM-D445 of the lubricating composition (VK40), it preferably, 30 mm ² / sec ~150mm ² / s, preferably in the range of from in the range of 35 mm ² / sec ~140mm ² / sec Can do.

  The lubricating composition can have a viscosity index (ASTM-D2270) in the range of 95-180, preferably 110-130.

  The pour point (ASTM-D97-93) of the lubricating composition can be −10 ° C. or lower, preferably −15 ° C. or lower, more preferably −20 ° C. or lower, and even more preferably −30 ° C. or lower.

  The lubricating composition has surprisingly good oxidative stability and preferably can exhibit the oxidation performance of a Group II base oil.

In some preferred embodiments of the present invention, a lubricating composition comprising an FT superheavy base oil and an alkylated aromatic blend stock includes:
FT ultraheavy base oil having a VK100 of at least 15 mm ² / sec, based on the total weight of the FT ultraheavy base oil and the alkylated aromatic blend stock; and FT ultraheavy base oil and alkylated aroma family blendstock total weight of 75 to 95% by weight, based in, consists or consist which comprises alkylated naphthalenes, alkylated aromatics blendstock having 4 mm ² / sec ~15mm ² / in the range of seconds VK 100;
Can be included.

In another preferred embodiment of the present invention, a lubricating composition comprising an FT superheavy base oil and an alkylated aromatic blend stock includes
FT ultraheavy base oil having a VK100 of at least 15 mm ² / sec, based on the total weight of the FT ultraheavy base oil and the alkylated aromatic blend stock, and a FT ultraheavy base oil and an alkylated aroma family blendstock total weight of 65 to 95% by weight, based in, consists or consist which comprises alkylated naphthalenes, alkylated aromatics blendstock with 11 mm ² / sec ~15mm ² / in the range of seconds VK 100;
Can be included.

  The FT superheavy base oil and the alkylated aromatic blend stock may comprise all of the lubricating composition, or preferably at least 95% or at least 98%, or at least 99% or at least 99.5% by weight of the total composition or At least 99.99% by weight may be comprised.

  The lubricating composition according to the invention further comprises antioxidants, antiwear additives, (preferably ashless) dispersants, cleaning agents, extreme pressure additives, friction modifiers, metal deactivators, corrosion inhibitors, One or more additives such as demulsifiers, antifoaming agents, seal compatible agents, additive diluent base oils and the like can be included. Such additives are usually present in small amounts.

  Those skilled in the art are familiar with these and other additives and will not be discussed in further detail here. Specific examples of such additives are described in, for example, Kirk-Othmer Encyclopedia of Chemical Technology, 3rd edition, vol. 14, p. 477-526.

  The lubricating composition can be used as a lubricant blend stock or in any suitable lubricating application. This can be particularly beneficial as a base oil blending component that requires a relatively high VK100, such as a monograde gas engine oil (SAE40 monograde). Here, current low sulfur base oils such as API Group II or Group III are sometimes borderline at VK100 and therefore have the problem of meeting SAE-J300 viscosity specifications for monograde.

  The lubricating composition can be formed by simply blending the ingredients as is known in the art. One preferred method of the present invention is that any FT superheavy base oil that fails the “Clarification” criteria (ASTM-D4176), passes the “Clarification” criteria (ASTM-D4176), and / or is defined above. Blending with an amount of alkylated aromatic blend stock to provide a lubricating composition having other properties.

  The invention also encompasses the use of alkylated aromatic blend stocks for the purpose of reducing waxy haze in FT superheavy base oils or precursor compositions comprising FT superheavy base oils. For this use, supply or provide a lubricating composition comprising FT superheavy base oil and alkylated aromatic blend stock with information or indication regarding the appearance of a clear appearance or absence of turbidity or low turbidity Can be included.

  The invention will now be further illustrated by the following non-limiting examples.

Example 1: Cloudiness:
The fluid properties and appearance of a lubricating composition comprising FT extra heavy base oil (XHBO) and an alkylated aromatic base stock were compared to that of the unblended components according to the following ASTM standard method.

Kinematic viscosity (ASTM-445): measured in cSt (mm ² / sec) at 40 ° C. and 100 ° C. (VK40 and VK100);
Viscosity index (ASTM-D2270): VI;
-Clarification criteria (ASTM-D4176) at atmospheric conditions (20 ° C);
-Pour point (ASTM-D97);
Cloud point (ASTM-D5773).

  A high pour point (high PPt) XHBO base stock was prepared substantially as described in Example 6 of US-8,152,869.

  According to the same process (the only difference was the temperature at which the dewaxing catalyst was operated), a low pour point (low Ppt) XHBO base stock was prepared. Higher temperatures result in more intense dewaxing and lower pour points.

  The resulting XHBO base stock had the properties shown in Table 1.

  The boiling range distribution of the XHBO base stock was analyzed according to ASTM-D7169. The carbon number distribution was also determined according to ASTM-D7169. The results are shown in Table 2.

  The alkylated aromatic blend stocks are alkylated naphthalenes and were obtained commercially from ExxonMobil Chemical Company under the trade names Synesstic® AN5 and Synesstic® AN12. These had the measured properties shown in Table 3 and a clear appearance.

  Twenty-three lubricating composition blends were prepared from XHBO and alkylated aromatic blend stock. Blend compositions and measured properties are shown in Tables 4-7.

  As shown, clear blends can be formulated with alkylated aromatic base stocks.

  Furthermore, the kinematic viscosity of all blends decreases at both 40 ° C. and 100 ° C. as the proportion of the relatively low viscosity alkylated aromatic blend stock increases, while the viscosity index VI remains generally constant, It is shown to be comparable to that of API Group II base oil (VI> 110).

  The synergistic behavior of the blends according to the present invention is further demonstrated by the improvement of the pour point (PPt) over the unblended alkylated aromatic base stock and XHBO base oil component. This is because the alkylated aromatic base stock can solubilize the waxy cloudy material in the FT superheavy base oil, and the FT superheavy base oil will allow any pour point of the alkylated aromatic basestock in the blend to It shows that it can be lowered below that of the above component.

Example 2: Oxidative stability:
To assess the oxidative stability of lubricating compositions according to the present invention, two prior art API Group II heavy intermediate viscosity grade base oils (Motiva Star 12 commercially available from Motiva Enterprises LLC, and HS Oil & Comparison with Formosa 500N), commercially available from Chemical International.

  As a suitable means to test the oxidation stability properties, the base oil / blend was formulated into industrial turbine oil. This was chosen because of the low additive processing speed involved, but the results can be applied to other industrial lubricants such as hydraulic fluids, or crankcase lubricants for various heavy duty diesel passenger cars. It will be possible. The additives used were as follows:

  Lubad 1128 is a patented industrial turbine oil additive comprising: (1) antioxidants such as N-phenylated naphthylamine, diphenylamine; and (2) corrosion inhibitors such as glycol ether derivatives, ethoxylated carboxylic acids and fatty acids; It is a package.

  Synative AC AMH-2 is a dual function additive: a low silica defoamer and a demulsifier (both are required for industrial turbine oils).

  Standard Rotating Pressure Vessel Oxidation Test (RPVOT): Previously measurements were made according to the RBOT test (ASTM-D2272).

  Four types of formulations were prepared as shown in Table 8. Table 8 also shows the results of the RPVOT test.

  The aromatic head group present in the alkylated naphthalene fluid is expected to result in oxidative brittleness of the blends containing it.

  As shown in Table 8, blends based on blends containing the alkylated aromatic blend stock components prepared in accordance with the present invention (Formulations 1 and 2) surprisingly have a typical API group II group. It was found to have oxidative stability comparable to that of the oil (Formulations 3 and 4). This provides further evidence of an unexpected beneficial synergistic effect of blending XHBO with an alkylated aromatic blend stock.

Claims (14)

A lubricating composition comprising an FT superheavy base oil and an alkylated aromatic blend stock, wherein the FT superheavy base oil has a kinematic viscosity at 100 ° C. ranging from 19 to 35 mm ² / sec.   The lubricating composition of claim 1, wherein the FT superheavy base oil has a low distillation temperature (T5) of at least 420 ° C and a high distillation temperature (T80) of at least 600 ° C. FT extra heavy base oil comprises a _{C 35+} hydrocarbon molecules of at least 95 wt% of _{C 30+} hydrocarbon molecules and at least 75 wt%, the lubricating composition according to claim 1 or 2.   The lubricating composition of any one of claims 1 to 3, wherein the FT superheavy base oil has a cloud point in the range of + 60 ° C to + 5 ° C and a pour point of -6 ° C or lower.   The lubricating composition according to any one of claims 1 to 4, wherein the FT superheavy base oil is a residual base oil.   The FT superheavy base oil has at least 55% by weight of the compound having at least 30 carbon atoms and at least 60 carbon atoms relative to the compound having at least 30 but less than 60 carbon atoms. 6. Lubricating composition according to claim 5, derived from a Fischer-Tropsch product wherein the weight ratio of the compound is at least 0.4.   Lubricating composition according to any one of claims 1 to 6, wherein the FT superheavy base oil is cloudy in the sense that it fails the "Clarification" criteria (ASTM-D4176-04) in the standard state.   8. Lubricating composition according to any one of claims 1 to 7, wherein the alkylated aromatic blend stock comprises alkylated aromatic naphthalene and / or alkylated aromatic benzene. Alkylated aromatic blend stock has a kinematic viscosity (ASTM-D445) at 100 ° C. in the range of 4 mm ² / sec ~15mm ² / s, the lubricating composition according to any one of claims 1-8.   10. Lubricating composition according to any one of claims 1 to 9, which passes the "clarification" standard (ASTM-D4176-04) at standard atmospheric conditions. (A) FT ultraheavy base oil having a VK100 of at least 15 mm ² / sec, from 5 to 25% by weight, based on the total weight of the FT ultraheavy base oil and alkylated aromatic blend stock; and (b) FT ultraheavy is configured on the total weight of the base oil and alkylated aromatics blendstock from or which contains an alkylated naphthalene 75 to 95 percent by weight based, alkylaromatic having 4 mm ² / sec ~15mm ² / ranging sec VK100 Tribe blend stock;
The lubricating composition according to claim 1, comprising:   Use of a lubricating composition according to any one of claims 1 to 11 for lubricating an engine, a compressor, a hydraulic pump, an industrial turbine, a gearbox or a power transmission system.   Production of a lubricating composition comprising blending an FT superheavy base oil that fails the “Clarification” criteria (ASTM-D4176) with an alkylated aromatic blend stock to provide a lubricating composition that passes the “Clarification” criteria. Method.   Use of an alkylated aromatic blend stock for the purpose of reducing waxy haze in a FT superheavy base oil or a precursor composition comprising an FT superheavy base oil.