ES2731850T3 - Base oil - Google Patents

Abstract

Base oil, characterized in that the base oil comprises branched saturated hydrocarbons having carbon numbers of at least C18, the 14C isotope content of the total carbon content in the base oil is at least 50% based on of the radioactive carbon content in the atmosphere in the year 1950 according to ASTM D 6866, contains at least 90% by weight of saturated hydrocarbons, less than 10% by weight of linear paraffins, not more than 0.1% by weight FIMS method of condensed polynaphthenes, 5-50% by FIMS method of mononaphthenes and at least 50% by weight of saturated hydrocarbons have a wide carbon number range of not more than 9 carbons and, being kinematic viscosity at 100 °C according to ASTM D445 from 3 cSt to 8 cSt, base oil volatility is not more than 2271.2*(VC100)-3.5373%.

Description

DESCRIPTION

Base oil

Technical field

The invention relates to a new base mother material. Specifically, the invention relates to a composition of saturated branched hydrocarbons and, in particular, to a composition based on biological raw materials, suitable for use as a high quality base oil or for use as a component in the production of a base oil that has a high viscosity index and good low temperature properties. The composition contains saturated branched hydrocarbons and has a narrow carbon number range.

State of the art

Base oils are commonly used for the production of lubricants, such as automobile lubricating oils, industrial lubricants and lubricating greases. These are also used as process oils, white oils and metal work oils. The finished lubricants consist of two general parts, lubricating base oils and additives. Base oils are the main constituents in finished lubricants and these contribute significantly to the properties of the finished lubricant. In general, some base oils are used to make a wide variety of finished lubricants by varying the mixtures of individual base oils and individual additives. The classification of the base oils of the American Petroleum Institute (API) is shown in Table 1. Today, API III Group III and IV base oils are used in high quality lubricants.

Table 1 API base oil classification

Group III oils are base oils with very high viscosity indices (VHVI) produced by modern methods from crude oil by hydrocracking, followed by isomerization of waxy linear paraffins to give branched paraffins. Group III oils also include base oils produced from crude paraffin wax paraffins (SW) of mineral oils. Future products, not yet available, prepared from waxes (GTL waxes) obtained by means of Fischer-Tropsch (FT) synthesis, for example, from charcoal or natural gas using the corresponding isomerization techniques, can also belong in the future to this group. Group IV oils are synthetic polyalphaolefins (PAO). Ester base oils belonging to Group V are produced from fatty acids and alcohols. Said fatty acids are natural or synthetic mono or dicarboxylic acids. Depending on the ester to be produced, the alcohol is a polyol or a monohydric alcohol. The ester base oils are normally monoesters, diesters, polyol esters or dimer esters. The ATIEL, Technical Association of the European Lubricant Industry (Association Technique de l'Industrie Européenne des Lubrifiants or Technical Association of the European Lubricants Industry), also uses a similar classification, which also includes Group VI: polyinternalolefins (IOP) ). In addition to the official classification, Group II + is also commonly used in this field, this group comprising saturated and sulfur-free base oils that have viscosity rates of more than 110, but below 120. In these classifications, hydrocarbons Saturated include paraffinic and naphthenic compounds, but not aromatic.

A definition of base oils (base mother materials) according to API 1509 is also available as: "A base mother material is a lubricant component that is produced by a single manufacturer with the same specifications (regardless of the power supply or the location of the manufacturer); which meets the same specifications of the manufacturer; and which is identified by a unique formula, a product identification number or both.

The base mother materials can be manufactured using various different processes. "The base oil is the base mother material or the mixture of base mother materials used in the API licensed oil. The types of base mother material are 1) mineral oil (paraffinic, naphthenic, aromatic), 2) synthetic (polyalphaolefins, alkylated aromatics, diesters, polyol esters, polyalkylene glycols, phosphate esters, silicones) and 3) oil vegetable.

Already for a long time, especially, the automotive industry has required lubricants and, therefore, base oils with improved technical properties. Increasingly, specifications for finished first level lubricants require products with excellent low temperature and low volatility properties, along with the correct viscosity level. In general, first-level lubricating base oils are base oils that have a kinematic viscosity of about 3 cSt or greater at 100 ° C (VC100); a pour point (PV) of about -12 ° C or less; and a viscosity index (IV) of approximately 120 or greater. In addition to the low pour point (PV), low temperature fluidity of multigrade engine oils is also needed to ensure that the engine starts easily in low temperature conditions. Low temperature fluidity is demonstrated as an apparent viscosity in cold cracking simulation tests (CCS) between -5 and -40 ° C. Modern first-level base oils that have a VC100 of approximately 4 cSt should normally have a CCS viscosity at -30 ° C (CCS-30) of less than 1,800 cP and oils that have a VC100 of approximately 5 cSt they must have a CCS-30 lower than 2,700 cP; The lower the value, the better. In general, lubricating base oils should have a Noack volatility no greater than that of current light neutral conventional Group I or Group II oils. Currently, only a small fraction of manufactured base oils can be used in formulations to meet the latest and most demanding lubricant specifications.

It is no longer possible to produce lubricants that meet the specifications of the most demanding car manufacturers from conventional mineral base oils (Group I and also Group II of the API, in some cases). Normally, such oils often contain too high concentrations of aromatic compounds, sulfur and nitrogen and, in addition, they also have high volatility and a poor viscosity index. In addition, the response of mineral oils to antioxidant additives is often moderate.

Synthetic base oils (ODP; API Group IV) and so-called semi-synthetic oils (VHVI; API Group III) play an increasingly important role, especially in automobile lubricants, such as engine oils and gears The useful life of the lubricants is, desirably, as long as possible, thus avoiding frequent oil changes by the user and also allows prolonged maintenance intervals of the vehicles, for example, in Commercial transport In the last decade, the intervals of change of motor oil of passenger vehicles have increased five times, being in the best of 50,000 km. In high-power vehicles, engine oil change intervals are currently at the 100,000 km level. A similar "longer life" development can be observed in industrial lubricants.

Synthetic PAO type base oils are prepared by oligomerizing alphaolefin monomers, followed by hydrogenation to achieve fully saturated paraffinic base oils. PAO base oils have relatively high IV values and, at the same time, excellent low temperature properties, the PV being even below -60 ° C. Due to the precise distillation of the product, the volatilities of the products are low and the flash points are high. The production and use of PAO base oils are quite limited due to the limited availability of expensive raw material, alpha-olefins.

Largely refined base oils of the VHVI type are produced from crude oil by removing unwanted compounds. The most important stage is dewaxing, which means the removal of solid and long chain paraffins or, by modern technology, the conversion of said n-paraffins into liquid isoparaffins. GTL base oil is prepared by the isomerization of catalytically synthetic FT wax. In comparison with mineral oils, VHVI base oil products are more paraffinic and have a narrower distillation range, thus having a considerably higher IV, lower volatility and clearly better low temperature properties. The aromatic content of these oils is extremely low and, in addition, these are basically free of sulfur and nitrogen.

In addition to the technical requirements of vehicle engine technology, strict environmental requirements also lead the industry to develop more sophisticated base oils. Sulfur-free fuels and base oils are required in order to obtain the full effect of the new catalyst technologies in modern vehicles and to reduce emissions of nitrogen oxides, hydrocarbons and volatile particles, as well as to achieve a direct reduction of sulfur dioxide in the exhaust gases. Conventional mineral oils contain sulfur, nitrogen and aromatic compounds and are usually more volatile and therefore are more harmful to the environment than newer sulfur-free base oils. In addition, mineral oils are not suitable for new engines with sensitive catalyst materials.

The production of base oils is also influenced by the increasingly common approach to "life cycle assessment" (LCA). The objective of the LCA is to observe the environmental burden of the product "from birth to death". The LCA is the tool to find the most critical points and to allow the changes towards a prolonged life of the product and the minimum inconveniences for the environment associated with the production, use, handling and disposal of the product. Longer oil change intervals of high quality base oils result in decreased consumption of non-renewable crude oil and quantities Reduced hazardous waste oils.

Currently, the use of recycled oils and renewable raw materials in the production of lubricants is often an object of interest. The use of renewable raw materials of biological origin instead of non-renewable fossil raw materials in the production of hydrocarbon components is desirable, since fossil raw materials are exhaustible and their effect of greenhouse gases (GHG) in the Environment is harmful. Problems related to recycled oils include complicated purification and reprocessing steps to obtain high quality base oils. In addition, the development of a comprehensive logistics and recycling system is expensive.

So far, esters have been the only type of base oil of renewable and biological origin used in lubricants. The use of such esters is limited to a few special applications, such as chain saw oils, biohydraulic oils and metalworking oils. In normal automobile and industrial lubricants, esters are mainly used as additives. The high price also limits the use of esters. In addition, the esters used in motor oil formulations are not interchangeable with other esters without re-conducting expensive motor tests, even in cases where the chemical composition of the replacement ester is, in principle, totally similar. Instead, base oils that consist of pure hydrocarbon structures are partially interchangeable with each other. There are also some technical problems related to esters. As polar compounds, esters withstand a greater tendency to seal swelling than pure hydrocarbons. This has created several problems related to elastomers in hydraulic applications. In addition, ester base oils hydrolyze more easily producing acids, which in turn cause corrosion in the lubricating systems. In addition, an even greater disadvantage of esters is that the additives developed for non-polar hydrocarbon base oils are not effective in polar ester base oils.

Document FI 100248 presents a two-stage process in which the intermediate distillate is produced from vegetable oil by hydrogenating the carboxylic acids or triglycerides of the vegetable oil to produce linear normal paraffins, followed by the isomerization of said n- paraffins to give branched paraffins. The hydrogenation was carried out at a temperature ranging from 330 to 450 ° C, at a pressure greater than 3 MPa (30 bar) and the hourly liquid velocity (LHSV) being 0.5 to 5 l / h. The isomerization step was carried out between 200 and 500 ° C under high pressure and the LHSV being 0.1 to 10 l / h.

EP 774451 discloses a process for isomerization of fatty acids or fatty acid alkyl esters. Isomerization of alkyl esters of fatty acid or unsaturated fatty acids is performed using clay or other cationic catalyst. In addition to the main product, dimers of feedstock material are obtained. After distillation, fatty acid alkyl esters or unsaturated branched fatty acids are obtained as product.

GB 1524781 discloses a process for the production of hydrocarbons from vegetable oil. In this process, the vegetable oil feed is pyrolyzed in three zones in the presence of a catalyst at a temperature of 300-700 ° C. In the process, hydrocarbons of the classes of gas, gasoline and diesel are obtained. These are separated and purified.

EP 209997 discloses a process for the production of base oils, which comprises the isomerization of waxy hydrocarbons based on crude oil, resulting in only minor amounts of light fractions. This process is used, for example, for the production of base oils belonging to Group III from waxy hydrocracking funds.

PAO processes are described in many patents. US 6,703,356 discloses a process using a large pore crystalline catalyst in the production of PAO base oil from 1-alkene monomers, which are normally produced from crude oil based ethylene. The present patent describes the use of higher α-olefin monomers, preferably C14 to C18, instead of the mixture of C10 (1-decene) or C8-C12 a-olefins normally used as starting material. The oligomerization of the α-olefins is followed by distillation of the product to give the desired viscosity fractions, followed by hydrogenation to give saturated "star-shaped" paraffins.

US 2005/0133408 discloses a base oil composition containing more than 10% by weight of cycloparaffins, which has a ratio of monocycloparaffins to polycycloparaffins of above 15, which also contains less than 0.3% by weight of aromatic compounds. The composition is obtained by subjecting the isolated paraffin wax obtained from the synthesis of Fischer-Tropsch to dewaxing by hydroisomerization and, finally, to hydro-finishing.

FI 66899 describes the use of fatty acid triglycerides and polymers thereof as base oil for lubricants. The double and ester bonds of the final product are unstable due to oxidation and hydrolytic cracking. The base oils according to said publication comprise unsaturated esters.

EP 03396078 presents a diesel fuel composition containing biocomponents, said composition comprising at least one component produced from a biological raw material of vegetable, animal or fish origin, diesel components based on crude oil and / or fractions of the Fischer-Tropsch process and, optionally, oxygen-containing components.

The use of starting materials containing heteroatoms of biological origin has not been indicated so far in the production of high quality saturated base oils or base oil components.

Based on the above teachings, it can be found that there is an obvious need for a base oil and a base oil component of biological origin, said branched saturated paraffin oil containing, and, furthermore, that it meets the highest quality requirements for base oils, the impacts of said oil being on the environment, for end users and for the saving of more favorable non-renewable raw materials compared to conventional mineral base oils, surpassing said base oil in a technical manner the Current products of the prior art.

Object of the invention

The present invention is disclosed in and by the appended claims.

A variety of the invention is to provide a new type of saturated base oil or a base oil component.

A further object of the invention is a base oil or a base oil component based on raw materials of biological origin.

A further object of the invention is a base oil or a base oil component based on raw materials of biological origin, said oils or base components meeting the quality requirements for the base oils t of Group II +, preferably at Group III of the API.

Another miscellaneous of the invention is to provide a saturated base oil or a base oil component based on raw materials of biological origin, the impacts of said oils or components being on the environment, for end users and for saving raw materials. more favorable non-renewable compared to conventional base oils based on crude oil.

The characteristic features of the base oil or the base oil component based on raw materials of biological origin according to the invention are presented in the appended claims.

General Description of the Invention

A base oil or a base oil component based on raw materials of biological origin according to the invention mainly comprises saturated branched hydrocarbons with a narrower carbon number range than the range of product distillates obtained by methods traditional. Said base oil or base oil component meets the quality requirements of Group II +, preferably Group III, of the API.

The term "saturated hydrocarbon / s", as used herein, refers to paraffinic and naphthenic compounds, not aromatic ones. Paraffinic compounds can be branched or linear. Naphthenic compounds are cyclic saturated hydrocarbons, that is, cycloparaffins. Such hydrocarbon with a cyclic structure is normally a derivative of cyclopentane or cyclohexane. A naphthenic compound may comprise an individual ring structure (mononaphthene) or two insulated ring structures (insulated dynaphthene) or two condensed ring structures (condensed dynaphthene) or three or more condensed ring structures (polycyclic nymphenes or polynaphtenes).

In this context, the term polyol refers to alcohols having two or more hydroxyl groups.

In this context, the width of the carbon number range refers to the difference in the carbon numbers of the largest and smallest molecules, plus one, in the final product.

In this context, fatty acids refer to carboxylic acids of biological origin, which have a carbon number greater than C1.

In this context, pressures are gauge pressures relative to normal atmospheric pressure.

Detailed description of the invention

Surprisingly, it was found that the high quality saturated base oil or the base oil component, which comprises branched saturated hydrocarbons having carbon numbers of at least C18 and having a narrow carbon number range, can be produce from source starting materials biological, said oils or components corresponding qualitatively to the base oils of Group II +, preferably Group III, of the API. The distillation range (ASTM D 2887) of the base oil or the base oil component of biological origin according to the invention starts above 250 ° C, the carbon number range and the boiling point range being extremely narrow and, in addition, the viscosity index being extremely high and, at the same time, the low temperature properties being good. The base oil or base oil component of biological origin according to the invention contains at least 90% by weight of saturated hydrocarbons, the proportion of linear paraffins being less than 10% by weight.

The width of the carbon number range of the base oil or base oil component of the invention is normally less than nine carbons. Typical carbon number ranges and typical structures of the base oils of the invention are presented in Table 2 below, the most typical number of carbons being bold.

The carbon numbers and carbon number ranges of the base oils or base oil components of the invention depend on the biological starting material used as the feedstock and, in addition, on the production process. In the structural examples of Table 2, the carbon number range of the base oil components 1 and 2 produced from a C16 / C18 feed by ketonization is normally from C31 to C35 and the carbon number range of the Component 3 of base oil produced from a C16 / C18 feed by condensation is normally from C32 to C36. These represent, both, the most common carbon number distribution of five carbon atoms. The feedstock material comprising an individual fatty acid chain length results in an extremely narrow carbon number range.

The biological base oil components of the invention presented in Table 2 are produced with the processes described below.

1. Isomerization of the fatty acid of pine oil to give a branched product, followed by ketoneization and, finally, hydrogenation.

2. Ketonization of a fraction of palm oil acid, followed by hydrogenation and, finally, isomerization.

3. Condensation of a C16 fatty acid distillate of palm oil, followed by hydrogenation and, finally, isomerization.

Table 2

(continuation)

Table 3 shows the carbon numbers and typical structures assumed of known synthetic mineral based hydrocarbon base oils that have a similar viscosity level. The carbon number range is determined by FIMS analysis. Naphthenes structures are typical examples of a group of compounds.

Table 3

(continuation)

The products in Table 3 are normally produced as follows:

1. PAO C10 is produced from 1-decene by oligomerization using a homogeneous catalyst. 2. SW is the isomerization product of the crude paraffin wax fraction based on mineral oil. 3. VHVI is hydrocracked and isomerized base oil derived from mineral oil.

Saturated hydrocarbons are classified as follows using the FIMS (field ionization mass spectrometry) method, according to carbon and hydrogen atoms:

1 C (n) .H (2n + 2) paraffins

2 C (n) .H (2n) mononaphtenes

3 C (n) .H (2n-2) dynaphthenes

4 C (n) .H (2n-4) trinaphthenes

5 C (n) .H (2n-6) tetranaphthenes

6 C (n) .H (2n-8) pentanaphthenes

In Tables 2 and 3, the percentages (% by FIMS) refer to the groups of compounds determined according to said method.

With respect to molecular structures, the base oils or base oil components of the invention differ from the products of the prior art, as shown in Tables 2 and 3. The PAO base oil of the prior art It mainly comprises long alkyl branches (> 4 carbons) (structure 1 in Table 3). In the SW isomerization products of the prior art (structure 2 in Table 3), the short branches are normally at the end of the hydrocarbon structure. The base oils or base oil components of the invention shown as structures 2 and 3 in Table 2 are very similar to SW base oils, but SW base oil contains a markedly higher amount of mononaphtenes and also of condensed dynaphtenes.

When isomerization is performed based on the double bonds of the fatty acid structure (structure 1 in Table 2), there are usually 1 to 4 carbon alkyl branches within the product hydrocarbon chain. Branched components are mixtures of isomers that differ with respect to branching sites.

Branches within the hydrocarbon chain decrease the pour point considerably more than those at the ends of the chain. In addition to the location of the branches, their number influences the point of discharge. The pour point decreases as the number of side chains increases, which, simultaneously, results in a decrease in the viscosity index. In the products of the invention, the relatively high proportion of the isomerized molecules contains more than 30 carbon atoms. Such high molecular weight compounds also normally have a high IV, although the pour point (PV) is decreased below -20 ° C.

As a result of cracking and hydrogenation of multi-ring aromatic compounds, there are also polynaphtenes fused with 3-5 rings (structure 3 in Table 3) in the VHVI products of the prior art, however, they are not present in the product of the invention. Condensed naphthenes make the PV-IV ratio more deficient than the alkyl branches. The best PV-IV correlation can be achieved by the optimal number of branches in the correct positions.

The product of the invention obtained by isomerizing paraffin wax from hydrodeoxygenated ketone (structure 2 in Table 2) is a branched product with a lower amount of methyl branching at the ends of the hydrocarbon chain and more branching. of methyl or ethyl within the hydrocarbon structure. Said base oil normally comprises some mononaphtenes, but not condensed dynaphtenes or polynaphtenes. Said mononaphtenes are formed as a result of the reactions of the double bonds of the fatty acid carbon chain or in an isomerization reaction, thus differing with respect to their structure from the naphthenes obtained by hydrogenating aromatics and cracking of polinaphtenes in mineral oil.

The product obtained using the condensation reaction, whether with aldol condensation, alcohol condensation (Guerbet reaction or the radical process, comprises a branching of methyl in the middle part of the main hydrocarbon chain (structure 3 in the Table 2) The product differs from the VHVI and SW isomerization products of the prior art (structures 3 and 2 in Table 3), said oils normally having branches mainly at the ends of the chains.

The base oil or base oil component according to the invention comprises a product produced from starting materials of biological origin, said product containing less than 10% by weight, preferably less than 5% by weight and particularly and preferably less than 1% by weight of linear paraffins; at least 90% by weight, preferably at least 95% by weight and in particular and preferably at least 97% by weight, in the best case at least 99% by weight, of saturated hydrocarbons, such as It is determined by a gas chromatography (GC) test.

The product of the invention contains 5-50, preferably 5-30, particularly and preferably 5-15 and in the best case 5-10% in FIMS by means of the FIMS of mononaphtenes; and less than 0.1% by weight in FIMS of polynaphtenes, as determined by the FIMS method.

As for said base oil or base oil component, the IV is greater than 115 and preferably greater than 130, particularly and preferably greater than 140 and in the best case greater than 150, as determined by the method of ASTM D 2270, together with the pour point that is not greater than -9 ° C, preferably is not greater than -12 ° C and particularly and preferably is not greater than -15 ° C (ASTM D 5950).

The dynamic viscosity at low temperature, CCS-30, for said base oil or base oil component is not more than 29,797 * (VC100) 27848 cP, preferably not more than 34,066 * (v C100) 23967 cP; CCS-35 is not greater than 36,108 * (VC100) 3069 cP, preferably it is not greater than 50,501 * (VC100) 24918 cP, as measured by the method of ASTM D 5293; the pour point being below -9 ° C, preferably below -12 ° C and particularly and preferably below -15 ° C (AST ^m D 5950).

As for said base oil or base oil component, the volatility of the product, which has a VC100 of 3 cSt at 8 cSt, is not greater than 2,271.2 * (VC100) '35373% by weight, as determined by the method of DIN 51581-2 (mathematical Noack method based on the distillation of GC from ASTM D 2887).

The carbon number range of the base oils or the base oil components of the invention is not more than 9 carbons, preferably not more than 7 carbons, particularly and preferably not more than 5 carbons and in the best of The cases are not greater than 3 carbons, as determined by the FIMS method. More than about 50%, preferably more than about 75% and particularly and preferably more than about 90% by weight of the base oil contains hydrocarbons belonging to this narrow carbon number distribution.

The distillation range of the base oils or the base oil components of the invention is not more than 150 ° C, preferably not more than 100 ° C, particularly and preferably not more than 70 ° C and at best cases not greater than 50 ° C (determined by the method of ASTM D 2887, with distillation points D10 and D90).

The sulfur content of said base oil or base oil component is less than 300 ppm, preferably less than 50 ppm, particularly and preferably less than 10 ppm and in the best case less than 1 ppm, as determined by the method of ASTM D 3120.

The nitrogen content of said base oil or base oil component is less than 100 ppm, preferably less than 10 ppm and particularly and preferably less than 1 ppm, as determined by the method of ASTM D 4629.

Said base oil or base oil component contains 14C carbon isotope, which can be considered as an indication of the use of renewable raw materials. The typical 14C isotope content of the total carbon content in the product, which is completely of biological origin, is at least 100%. The content (proportion) of 14C carbon isotope is determined based on the radioactive carbon content (14C carbon isotope) in the atmosphere in 1950 (ASTM D 6866). The 14C isotope content of the base oil according with the invention it is lower in cases where other components than components other than biological components are used in the processing of the product, said content being, however, greater than 50%, preferably greater than 90%, particularly and preferably greater 99% In this way, even low amounts of base oil of biological origin can be detected in other types of hydrocarbon base oils. The base oil or base oil component of the invention can be prepared from feedstock material that originates from starting material of biological origin, called biological starting material in the present description. The biological starting material is selected from the group consisting of: a) fats, oils, vegetable waxes; fat oils, animal waxes; fats, oils, fish waxes, and b) fatty acids or free fatty acids obtained from vegetable fats, vegetable oils, vegetable waxes; animal fats, animal oils, animal waxes; fish fats, fish oils, fish waxes and mixtures thereof by hydrolysis, transesterification or pyrolysis, and

c) esters obtained from vegetable fats, vegetable oils, vegetable waxes; animal fats, animal oils, animal waxes; fish fats, fish oils, fish waxes and mixtures thereof by transesterification, and

d) metal salts of fatty acids obtained from vegetable fats, vegetable oils, vegetable waxes; animal fats, animal oils, animal waxes; fish fats, fish oils, fish waxes and mixtures thereof by saponification, and

e) fatty acid anhydrides of vegetable fats, vegetable oils, vegetable waxes; animal fats, animal oils, animal waxes; fish fats, fish oils, fish waxes and mixtures thereof, and f) esters obtained by esterification of free fatty acids of vegetable, animal or fish origin with alcohols, and

g) fatty alcohols or aldehydes obtained as fatty acid reduction products from vegetable fats, vegetable oils, vegetable waxes; animal fats, animal oils, animal waxes; fish fats, fish oils, fish waxes and mixtures thereof, and

h) recycled food grade fats and oils, and fats, oils and waxes obtained by genetic engineering, and

i) mixtures of said starting materials.

Biological starting materials also include the corresponding compounds derived from algae and insects, as well as starting materials derived from aldehydes and ketones prepared from carbohydrates. Examples of suitable biological starting materials include fish oils, such as Baltic herring oil, salmon oil, herring oil, tuna oil, anchovy oil, sardine oil and mackerel oil; Vegetable oils, such as rapeseed oil, rapeseed oil, canola oil, pine oil, sunflower seed oil, soybean oil, corn oil, hemp oil, olive oil, cottonseed oil , mustard oil, palm oil, peanut oil, castor oil, jatropha seed oil, palm kernel oil and coconut oil; and, in addition, animal fats, such as lard, tallow, and also recycled food grade fats and oils, as well as fats, waxes and oils produced by genetic engineering are also suitable. In addition to fats and oils, suitable starting materials of biological origin include animal waxes, such as beeswax, Chinese wax (insect wax), lacquer wax and lanolin (wool wax), as well as vegetable waxes, such as carnauba palm wax, ouricouri palm wax, jojoba seed wax, candelilla wax, esparto wax, Japanese wax and rice bran oil.

The biological starting material may also contain free fatty acids and / or fatty acid esters and / or metal salts thereof or cross-linked products of the biological starting material. Said metal salts are normally alkaline earth metal or alkali metal salts.

The base oil or base oil component of the invention, comprising hydrocarbons that normally have a carbon number of at least 18, can be produced from biological starting materials by methods that result in chain elongation. carbon from the molecules of the starting material to the level necessary for base oils (> C18). Suitable methods include processes based on condensation reactions, which mean reactions based on the functionality of the feed molecules, in combination with at least one of the following: reduction or transesterification, hydrolysis, metathesis, decarboxylation, decarbonylation processes or reactions. , isomerization, dewaxing, hydrogenation and finishing. Condensation reactions include, for example, decarboxylation condensation (ketonization), aldol condensation, alcohol condensation (Guerbet reaction) and reactions on double bonds that include dimerization, trimerization, oligomerization and radical reactions. The hydrocarbons, preferably saturated hydrocarbons, are obtained as a product by processing the biological starting materials, followed, when necessary, by the fractionation of said hydrocarbons by distillation to obtain final products.

In the method based on ketone reactions, the fatty acid acid groups react with each other to give ketones. Ketonization can also be carried out with fatty acid esters, acid anhydrides fatty, fatty alcohols, fatty aldehydes, natural waxes and fatty acid metal salts. The ketone obtained is reduced by giving a paraffin, followed by isomerization, to improve the low temperature properties of the final product. Isomerization is optional in cases where the branched feedstock is subjected to ketonization. In the ketonization stage, dicarboxylic acids or polyols, including diols, can also be used as the starting material, which allows for greater chain elongation than with fatty acids only. In that case, a polyketonic molecule is obtained, which is processed similarly to the monoketone. In the ketone reaction, the pressure is between 0 and 10 MPa, the temperature being between 10 and 500 ° C, and, in addition, supported metal oxide catalysts are used, the metal being preferably molybdenum, nickel-molybdenum, manganese , magnesium, calcium or cadmium; silica and / or alumina can be used as support. Particularly and preferably, the metal in the metal oxide is molybdenum, manganese and / or magnesium in a catalyst without support.

In the aldol condensation reaction, the aldehydes and / or ketones are condensed to substantially increase the carbon number of the hydrocarbon stream. Saturated aldehydes are preferably used as feedstock material. In the process, branched unsaturated aldehydes or ketones are obtained. The catalyst is preferably an alkali metal or alkaline earth metal hydroxide, for example, NaOH, KOH or Ca (OH) ² , the temperature then being 80 to 400 ° C, preferably, a lower temperature is used with the lower molecular weight feeds and higher temperatures with the higher molecular weight feed. The amount of catalyst used in the homogeneous reaction ranges from 1 to 20%, preferably 1.5 to 19%, by weight.

In the condensation reaction with alcohol, in particular the Guerbet reaction, the alcohols are condensed to substantially increase the number of carbons in the hydrocarbon stream, thereby obtaining branched and branched polyfunctional monofunctional alcohols, respectively, of alcohols. of monohydroxy and polyhydroxy in the condensation reaction of alcohols. Saturated alcohols are preferably used as feedstock. Known catalysts of the Guerbet reaction, such as alkali metal and alkaline earth metal hydroxides and alkoxides, or metal oxides in combination with a cocatalyst can be used as reaction catalysts. The amount of the catalyst used in the reaction varies from 1 to 20%, preferably from 1.5 to 19%, by weight. Suitable cocatalysts include salts of chromium (III), manganese (III), iron (II), cobalt (II) or lead (II) or static oxide or zinc oxide, the salts being salts soluble in water or alcohols, preferably sulfates The cocatalyst is used in amounts ranging between 0.05 and 1%, particularly and preferably between 0.1 and 0.5%, by weight. The alkali metal hydroxides, together with the zinc oxide that serves as cocatalyst, are preferably used in the reaction. Chain elongation by means of the alcohol condensation reaction is carried out between 200 and 300 ° C, preferably between 240 and 260 ° C, the reaction being carried out at the vapor pressure provided by the alcohols present in the reaction mixture . Water is released in the reaction, said water separating continuously.

In the radical reaction, the carbon chains of saturated carboxylic acids are elongated with alpha olefins. In the radical reaction step, the feedstock material comprising saturated carboxylic acids and alpha olefins in a 1: 1 molar ratio is reacted between 100 and 300 ° C, preferably between 130 and 260 ° C, at the pressure of vapor provided by the reaction mixture, in the presence of an alkyl peroxide catalyst, peroxy ester, diacyl peroxide or peroxicetal. Preferably, alkyl peroxides are used, such as diterciate butyl peroxide catalysts. The amount of the catalyst used in the reaction is 1 to 20%, preferably 1.5 to 10%, by weight. A branched carboxylic acid is obtained as the reaction product.

In electrochemical synthesis, carboxylic acids, in particular, fatty acids in vegetable oils, are first extracted, followed by the formation of carboxylic acid salts by dissolving them in methanol or aqueous methanol solution, which contains the 10-20% by weight of potassium hydroxide for the neutralization of carboxylic acids, in order to form an electrolyte solution for electrochemical oxidation. The salts are transformed into long chain hydrocarbons by the reaction known as Kolbe synthesis. The carbon number of the product obtained is a carbon lower than that obtained using the ketone reaction.

The reduction of the product obtained from the hydrocarbon chain (paraffin) elongation step is carried out by hydrogenation, thereby removing the polarity due to the oxygen atoms, and, in addition, the oxidation stability is improved by the saturation of any double bond. In hydrogenation, the product of the chain elongation reaction and hydrogen gas are passed to the hydrogenation reactor at a pressure normally between 1 and 15 MPa and the temperature of 150 to 400 ° C. In the hydrogenation stage, special catalysts containing Group VIII metals and / or VIA of the periodic system of the elements on a support can be used. The hydrogenation catalyst is normally a catalyst of Pd, Pt, Ru, Rh, Ni, NiMo or CoMo supported, the support being activated carbon, alumina and / or silica. After reduction, the branched methyl paraffinic wax is obtained from the other feeds, but the ketoneization of the unbranched feed components.

The low temperature properties of the product can be improved by isomerization. In isomerization, the linear hydrocarbons become branched and the solid paraffins therefore become liquid.

In isomerization, hydrogen gas and paraffinic components are reacted in the presence of an isomerization catalyst. In the isomerization stage, the pressure is normally between 1 and 15 MPa, the temperature being normally between 200 and 400 ° C. Special catalysts containing molecular sieves and a Group VIII metal from the periodic system of the elements, such as Ni, Pt and Pd, can be used. Alumina and / or silica can serve as support. Isomerization is not necessary if branched structures are obtained from the chain elongation reaction and if the pour point of the product is sufficiently low.

Products produced from biological starting materials using the methods described above mainly comprise saturated hydrocarbons and mixtures thereof. These can be used as base oils and as components for the production of base oils, depending on what the desired properties of the base oil are. The high quality base oil or a Group II + base oil component, preferably Group III, of the API is obtained as a product, said base oil or base oil component being particularly suitable for the production of high lubricants quality, white oils, process oils and oils for metal work fluids.

Advantages of the invention

The base oil or the base oil component of the invention is endowed with superior technical properties, compared to conventional hydrocarbon oils of the corresponding viscosity class. The narrow boiling range indicates that the product does not contain any initial light fraction (which means that the molecules are considerably lighter than average), which is shown by decreased product volatility. This results in lower oil consumption and reduced emissions in practical applications. The "tail" composed of the heaviest components (meaning that the molecules are considerably heavier than average) is also missing. This results in excellent low temperature properties of the product.

As for the base oil or base oil component of the invention, the range of carbon number and boiling point can be adjusted to the desired range by selecting the composition of the feedstock material. As for the base oils of the prior art, the boiling point range is adjusted by distilling the product to obtain a fraction having the desired kinematic viscosity. It is preferable that the lubricants comprise base oils with narrow carbon number ranges and, therefore, narrow boiling ranges. In this way, the base oil contains molecules of similar sizes that behave under different conditions in a similar manner.

The base oil or base oil component of the invention consists mainly of isomerized paraffins, the remainder being mononaphthenes and, to a lesser extent, non-condensed dynaphtenes. It is known that mononaphthenic compounds and also non-condensed dynaphtenes have physical properties similar to isoparaffins. Condensed naphthenes, in the prior art products, have a lower IV and poor temperature viscosity properties, as well as more poor oxidation stability.

As regards the base oil or base oil component of the invention, the high IV of the product means, in practice, that the amount of the viscosity index improver, component VII, normally used in the compositions of Lubricant oils. In general, it is known that, for example, in engine oils, component VII is the main cause of deposits in the engine. In addition, reducing the amount of VII results in significant savings in formulation costs.

In contrast to conventional products derived from crude oil, no sulfur, nitrogen or aromatic compound is present in the base oil or base oil component of the invention, which allows safe use thereof in such applications in that users are exposed to oil or oil vapor. In addition, the response of the product of the invention to antioxidants and pour point depressants (PPDs) is excellent, thus allowing the prolongation of the useful life of lubricants prepared from said oil. base, as well as the use of it at lower temperatures.

In comparison with esters or other base oils containing heteroatoms, the base oil or base oil component of the invention is more stable with respect to hydrolysis, that is, it will not readily decompose releasing corrosive acids in wet conditions. The base oil of the invention is also chemically more stable than the more reactive ester base oils and, in addition, the oxidation resistance thereof is improved, compared to the ester base oil derived from unsaturated fatty acids of origin biological.

In comparison with esters, the base oil or non-polar base oil component of the invention is more compatible with the conventional oil base oil components derived from crude oil, the base oil components obtained from the process of Fischer-Tropsch, as well as with lubricant additives. In addition, there are no such problems with elastomers, such as the sealing materials found with the esters.

The advantages of the base oil or base oil component of the invention include the fact that it meets the requirements of the base oils according to Group II +, preferably Group III, of the API and can be used in compositions of automotive engine oil like other base oils of the API classification, in accordance with the same basic oil exchange standards.

The base oil or base oil component of the invention is derived from renewable natural resources as can be analyzed from the ¹⁴ C isotope content of the product.

In accordance with the invention, renewable biological raw materials constitute a completely novel resource of raw materials for high quality saturated hydrocarbon base oils or base oil components. Carbon dioxide emissions that contribute to the greenhouse effect can also be reduced through the use of renewable raw materials, rather than non-renewable resources.

In the following, the invention is illustrated by means of the following examples without wishing to limit the scope thereof.

Examples

In Examples 1 to 5, paraffinic hydrocarbons with long chains are produced from biological starting materials that contain oxygen by means of a ketone-based process. The products are very suitable as base oils or base oil components without mixing limitations and, in addition, the products are also compatible with lubricant additives. In Example 6, the detection of the proportion of the base oil of biological origin in the traditional mineral base oil is shown. Table 4 shows the properties of the base oil components prepared in Examples 1 to 5 from biological starting materials and Table 5 shows the properties of the prior art products.

Example 1

Preparation of a hydrocarbon component from a fraction of stearic acid

A mixture of vegetable oils (flaxseed, soybean, sunflower and rapeseed oils) was hydrolyzed and the fatty acids were distilled to obtain product fractions according to carbon numbers. The double bonds of the fatty acid fraction used as feed were previously selectively hydrogenated. The stearic acid fraction (C ¹⁷ H ³⁵ COOH) thus obtained was diluted with a paraffinic diesel fuel based on biological raw material. The stearic acid content of the mixture was 31% by weight. The feedstock material was ketone in a continuous tube reactor using an MnO ² catalyst. The reactor temperature was 370 ° C and the WHSV was 3. 18-pentatriacontanone, that is, stearone, was obtained as a product in a diluent.

In the hydrogenation step, said stearone / diluent mixture obtained was hydrogenated in a high pressure Parr reactor using a dried and activated NiMo / A ^ O ³ catalyst to obtain linear paraffin. The ketone was hydrogenated at 330 ° C at a pressure of 5 MPa until no ketone peak was present in the IR spectrum of a sample, the mixing speed being 300 rpm. Stearic acid resulted in a linear C35 paraffin. The linear paraffin wax obtained from the ketone was isomerized in a Parr reactor to obtain a branched paraffin of the base oil class, using reduced Pt / AhO ³ molecular sieve as catalyst. The previously obtained heated paraffin / diluent mixture was isomerized at a hydrogen pressure of 3 MPa and at 340 ° C until a PV of -6 ° C was obtained. Finally, the light fractions were removed by vacuum distillation, followed by finishing the paraffinic product by filtration through diatomite.

Example 2

Preparation of a hydrocarbon component from fatty acids derived from palm oil

The palm oil was hydrolyzed and the double bonds selectively hydrogenated. After hydrogenation, the fatty acid composition was as follows: 1% C14, 44% C16, 54% C18 and 1% C20, all percentages being by weight. The fatty acids were ketone as in Example 1 and the ketone was followed by solvent removal by distillation.

In the hydrogenation step, the ketone mixture obtained above was hydrogenated in a Parr reactor using a dried and activated NiMo / AhO ³ catalyst to give a linear paraffin. The ketone mixture was hydrogenated at a pressure of 3.3 MPa, at 340 ° C, the mixing speed being 300 rpm. Palm oil resulted in a linear paraffin.

N-paraffin was obtained from the ketone mixture, by hydrogenation, isomerized in a Parr reactor at 340 ° C at a hydrogen pressure of 3 MPa to give a branched paraffin of the oil viscosity class of base, using a molecular sieve catalyst of reduced Pt / A ^ Os until the PV point was below -15 ° C. Finally, the light fractions were removed by distillation under reduced pressure.

Example 3

Preparation of a hydrocarbon component from fatty acid methyl esters

The purified animal fat was transesterified in two stages with methanol under alkaline conditions at 70 ° C at a pressure of 0.1 MPa, thereby obtaining fatty acid methyl esters. Sodium methoxide served as a catalyst. The reaction mixture was purified by washing with acid and water. Finally, the mixture of fatty acid methyl esters was dried.

The mixture of fatty acid methyl esters was diluted with a paraffinic diesel fuel of biological origin. The fatty acid methyl ester content of the feedstock material obtained was 30% by weight and the feedstock material was ketone in a continuous tube reactor, as disclosed in Example 1. Thus, they were obtained both saturated and unsaturated ketones as products.

In the hydrogenation step, the ketone mixture obtained above was hydrogenated in a Parr reactor as in Example 2. Isomerization was also performed as in Example 2.

Example 4

Preparation of a hydrocarbon component from pine oil based on isomerized fatty acids The mixture of fatty acids from distilled pine oil was isomerized using a mordenite catalyst in a Parr reactor. H mordenite zeolite served as catalyst and water was used in an amount of 3% by weight of the total mass of the reaction mixture.

The mixture was purged with nitrogen. The isomerization temperature was 280 ° C, the nitrogen pressure was 2.0 MPa and the mixing speed was 300 rpm. The catalyst was removed by filtration, followed by distillation of the monomeric acids of the product under reduced pressure.

The double bonds of the monomeric acids were selectively hydrogenated in a Parr reactor using a Pd / C catalyst. Hydrogenation was carried out at 150 ° C, at a hydrogen pressure of 1.8 MPa. Linear fatty acids were removed from the mixture by adding a double amount of hexane, followed by cooling the mixture to -15 ° C and removing the crystals formed by filtration. Finally, the solvent was removed by filtration of the isostearic acid fraction.

The iso-stearic acid fraction was diluted with a paraffinic diesel fuel of biological origin in a ratio of 30 to 70% by weight. The feedstock material was ketone in a continuous tube reactor using an MnO ² catalyst. The reactor temperature was 370 ° C, the WHSV being 1.7. Therefore, a mixture of isomerized ketones was obtained as a product.

In the hydrogenation step, the ketone mixture thus obtained was hydrogenated in a Parr reactor as in Example 2. The solvents were removed by filtration of the final product under reduced pressure. Subsequently, n-paraffins were extracted from the product by the solvent dewaxing method and, finally, the paraffinic product was finished by filtration through diatomite. Mainly branched paraffins were obtained as the final product.

Example 5

Preparation of a hydrocarbon component from pine oil based on isomerized fatty acids and dicarboxylic acid

The stearic acid fraction prepared according to Example 4 and the C6 dicarboxylic acid (adipic acid) were mixed in a 1: 3 molar ratio. The feed mixture was ketone in a Parr reactor using a MgO catalyst. The acid mixture was ketone at 340 ° C, using a mixing speed of 300 rpm. In the hydrogenation step, the ketone mixture obtained in this way was hydrogenated in a Parr reactor as in Example 1 and the light fractions were removed by filtration of the final product under reduced pressure. As a product, branched paraffins were obtained that had longer chains compared to the other examples.

Summary of Examples 1 - 5

Proceeding as in Examples 1-5, the base oil components can also be produced from other fats and vegetable oils, from fish, animals or from recycled foods (e.g. frying oils) or esters or soaps derived from fatty acids of said fats and oils or the corresponding free alcohols and fatty acids. The hydrocarbon components can also be produced from natural waxes consisting of fatty acids and alcohols by the process in a similar manner. On the other hand, the corresponding alcohols can be prepared from fatty acids using, for example, a Ru / C catalyst and said alcohols can be traditionally esterified with fatty acids. The esters of the number of C36 carbons are thus obtained for ketoneization, while the natural waxes are normally C38-C46 esters.

Example 6

Preparation of a hydrocarbon component from C16 alcohol derived from vegetable oil

In the condensation reaction, 200 g of C16 fatty alcohol, palladium chloride (5 ppm palladium) and 12 g of sodium methoxylate were weighed in a Parr reactor. Mixing was set at 250 rpm, temperature at 250 ° C and pressure at 0.5 MPa. A slight nitrogen purge was maintained to sweep the water released in the reaction. The reaction was carried out until the amount of condensed alcohol was stabilized in the GC analysis. After the reaction, the product was neutralized with hydrochloric acid, washed with water and dried with calcium chloride.

In the next HDO stage, the condensed alcohol obtained above was hydrogenated in a high pressure Parr reactor using a dried and activated NiMo / A ^ Oa catalyst, to give a branched methyl paraffin. The aldehyde was hydrogenated at 340 ° C, at a pressure of 5 MPa, mixing at 300 rpm until no alcohol spike was detected in the FTIR spectrum. The pour point of the branched methyl wax was 69 ° C. The C32 paraffin wax obtained above was isomerized in a Parr reactor to give a branched paraffin of the base oil class using a reduced Pt / A ^ Oa molecular sieve catalyst. The previously heated paraffin was isomerized at a hydrogen pressure of 3 MPa and at 340 ° C until a pour point of below 15 ° C was obtained. Finally, the light fractions were distilled from the product under reduced pressure. The properties of the condensed, hydrodeoxygenated and hydroisomerized base oil are provided in Table 3. Similar hydrocarbon compounds can be produced by other condensation reactions and in radical reactions in the same manner.

Table 4

Table 5

Example 7

Preparation of a hydrocarbon component from fatty acids derived from palm oil

Palm oil was hydrolyzed. The fatty acids derived from palm oil were used as feedstock material after selective prior hydrogenation of the double bonds of said fatty acids. The fatty acids were vaporized with nitrogen purge in a separate vaporizer unit and were continuously ketone at atmospheric pressure, in a tubular reactor using a MnO ² as catalyst. The reactor temperature was 380 ° C, the WHSV of the feed being 11 / h-1.

The ketone mixture C31, C33, C35 obtained from the ketonization phase was continuously deoxygenated in a tubular fixed bed reactor using a NiMo / AhO ³ catalyst dried and activated to give linear paraffins. Hydrodeoxygenation was carried out at a pressure of 4 MPa (40 bar), at 270 ° C and with a WHSV of 11 / h.

The linear paraffin wax obtained in the HDO stage was continuously isomerized in a tubular fixed bed reactor using a reduced Pt / Al ² O ³ molecular sieve catalyst to give branched paraffins using a reduced Pt molecular sieve catalyst. / Al ² O ³ . The isomerization was performed at 340 ° C, at a hydrogen pressure of 4 MPa until the pour point of the product was below -15 ° C. Finally, the light fractions were distilled under reduced pressure and separated.

Hydrocarbon components can also be produced similarly from other vegetable or fish oils and animal fats.

Table 6

Example 8

Determination of the biological origin of the hydrocarbon component

The hydrocarbon component of biological origin was weighed in mineral oil based on Group III base oil and mixed thoroughly. In the first sample, 0.5014 g of the hydrocarbon component of biological origin was weighed and the Group III base oil component was added in an amount to a total weight of 10,0000 g; In the second sample, 1.0137 g of the hydrocarbon component of biological origin was weighed and the Group III base oil component was added in an amount to a total weight of 10.0232 g. The measured results are summarized in Table 6, below. The radioactive carbon content is expressed as "percentage modern carbon", based on the radioactive carbon content of the atmosphere in 1950. At present, the radioactive carbon content of the atmosphere is approximately 107%. The value of S13 C shows the ratio of stable 13C / 12C carbon isotopes. Through this value, the isotope fractionation found in the process can be corrected. The actual results are presented in the last column.

Table 7

Example 9

Carbon number distribution

The proportion of the narrow carbon number distribution of the base oil product depends on the distillation. In Figure 1, the carbon number distributions of VHVI (cut at 413-520 ° C) and the base oils of the invention (cut at 360 ° C) are shown. The carbon number distribution of the base oils according to the invention is narrower than that of conventional base oils when the distillation is cut similarly to> 413 ° C, which corresponds to the C26 paraffin. The base oils of the invention contain a higher amount of higher boiling fractions, compared to the conventional product of the same viscosity range (VC100 at about 4 cSt), as shown in Figure 1 with carbon number distributions . Lower boiling components with carbon numbers <C31 are due to cracking in isomerization. Upper boiling compounds enhance IV.

Claims (15)

1. Base oil, characterized in that the base oil comprises branched saturated hydrocarbons having carbon numbers of at least C18, the 14 C isotope content of the total carbon content in the base oil is at least 50% On the basis of the radioactive carbon content in the atmosphere in the year 1950 according to ASTM D 6866, it contains at least 90% by weight of saturated hydrocarbons, less than 10% by weight of linear paraffins, not more than 0, 1% by means of the FIMS method of condensed polynaphtenes, 5 50% by the FIMS method of mononaphtenes and at least 50% by weight of the saturated hydrocarbons have the width of the carbon number range of no more than 9 carbons and , the kinematic viscosity being at 100 ° C in accordance with ASTM D445 from 3 cSt to 8 cSt, the volatility of the base oil is not greater than 2,271.2 * (VC100) '35373 %. 2. Base oil according to claim 1, characterized in that the 14 C isotope content is greater than 90%, preferably greater than 99%. 3. Base oil according to claims 1 or 2, characterized in that at least 75% by weight of the saturated hydrocarbons have the width of the carbon number range of no more than 9 carbons. 4. Base oil according to any one of claims 1-3, characterized in that the width of the carbon number range thereof is not more than 7 carbons, preferably not more than 5 carbons and particularly and preferably not more than 3 carbons 5. Base oil according to any one of claims 1-4, characterized in that it comprises at least 95%, preferably at least 97% and in the best case at least 99% by weight of saturated hydrocarbons . 6. Base oil according to any one of claims 1-5, characterized in that it comprises less than 5% and preferably less than 1% by weight of linear paraffins. 7. Base oil according to any one of claims 1-6, characterized in that it comprises 5-30% and preferably 5-15% mononaphtenes. 8. Base oil according to any one of claims 1-7, characterized in that it meets the requirements of the base oils according to the API Group III classification. 9. Base oil according to any one of claims 1-8, characterized in that the viscosity of CCS-30 of said base oil is not greater than 29,797 * (VC100) 27848 cP, preferably it is not greater than 34,066 * (VC100) 23967 cP; The viscosity of CCS-35 is not greater than 36,108 * (VC100) 3069 cP, preferably it is not greater than 50,501 * (VC100) 24918 cP; the pouring point not exceeding -9 ° C, preferably not exceeding -12 ° C and particularly and preferably not exceeding -15 ° C. 10. Base oil according to any one of claims 1-9, characterized in that the viscosity index of said base oil is greater than 115, preferably greater than 130, particularly and preferably greater than 140 and in the best of cases over 150. 11. Base oil according to any one of claims 1-10, characterized in that it is derived from a starting material of biological origin selected from the group consisting of a) vegetable fats, vegetable oils, vegetable waxes, animal fats, animal oils, animal waxes, and fats, fish oils and waxes, and b) fatty acids or free fatty acids obtained from vegetable fats, vegetable oils, vegetable waxes, animal fats, animal oils, animal waxes, fish fats, fish oils, fish waxes and mixtures thereof by hydrolysis, transesterification or pyrolysis, and c) esters obtained from vegetable fats, vegetable oils, vegetable waxes, animal fats, animal oils, animal waxes, fish fats, fish oils, fish waxes and mixtures thereof by transesterification, and d) metal salts of fatty acids obtained from vegetable fats, vegetable oils, vegetable waxes, animal fats, animal oils, animal waxes, fish fats, fish oils, fish waxes and mixtures thereof by saponification, and e) fatty acid anhydrides of vegetable fats, vegetable oils, vegetable waxes, animal fats, animal oils, animal waxes, fish fats, fish oils, fish waxes and mixtures thereof, and f) esters obtained by acid esterification free fatty acids of vegetable, animal or fish origin with alcohols, and g) fatty alcohols or aldehydes obtained as products for the reduction of fatty acids from vegetable fats, vegetable oils, vegetable waxes, animal fats, animal oils, animal waxes, fish fats, fish oils, fish waxes and mixtures thereof, Y h) recycled food grade fats and oils, and fats, oils and waxes obtained by genetic engineering, and i) mixtures of said starting materials. 12. Base oil according to any one of claims 1-11, characterized in that it contains less than 10%, preferably less than 5% and particularly and preferably less than 1% by weight of aromatic carbon. 13. Base oil according to any one of claims 1-12, characterized in that the sulfur content thereof is less than 300 ppm, preferably less than 50 ppm, particularly and preferably less than 10 ppm and in the best of cases less than 1 ppm. 14. Base oil according to any one of claims 1-13, characterized in that the nitrogen content thereof is less than 100 ppm, preferably less than 10 ppm and particularly and preferably less than 1 ppm. 15. Base oil according to any one of claims 1-14, characterized in that the distillation range of said base oil is not more than 150 ° C, preferably not more than 100 ° C, particularly and preferably not greater 70 ° C and in the best case no greater than 50 ° C, with distillation points D10 and D90.