TR201908714T4 - Base oil. - Google Patents

Abstract

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

Description

DESCRIPTION BASE OIL Technical field The invention relates to a novel base stock material. Specifically, the invention relates to a composition of branched saturated hydrocarbons, and in particular, biological raw materials, suitable for use as a high-quality base oil or as a component in the production of a base oil with a high viscosity index and good low-temperature properties. The composition contains branched saturated hydrocarbons and has a narrow range of carbon numbers. State of the art Base oils are widely used in the production of mineral oils such as lubricating oils for automotive, industrial mineral oils, and lubricating greases. They are also used as process oils, white oils, and metalworking oils. Final mineral oils consist of two general components: lubricating base oils and additives. Base oils are the fundamental building blocks in final mineral oils and contribute significantly to the final oil's properties. Generally, several base oils are used to produce a wide variety of final mineral oils by varying the mixtures of individual base oils and additives. The American Petroleum Institute (API) base oil classification is shown in Table 1. Currently, API Group III and IV base oils are used in high-quality mineral oils. Table 1. API base oil classification Group Saturated hydrocarbons Sulfur, wt-% (ASTM D Viscosity index (VI) wt-O/o (ASTM D V All other base oils not belonging to Group I - IV Group III oils are very high viscosity index (VHVI) base oils produced from crude oil by modern methods via hydrocracking followed by isomerization of waxy linear paraffins to obtain branched paraffins. Group V also includes oils from waxes obtained by Fischer-Tropsch (FT) synthesis (GTL waxes), for example from coal or natural gas, using corresponding isomerization techniques, which are not yet available and may also belong to this group in the future. Group IV oils are synthetic polyalphaolefins (PAO). Ester base oils belonging to Group V are derived from fatty acids and alcohols. They are produced. The fatty acids in question are natural or synthetic mono- or dicarboxylic acids. Depending on the ester to be produced, the alcohol is either a polyol or a monohydroxy alcohol. Ester base oils are typically monoesters, diesters, polyol esters, or dimer esters. A similar classification is also used by ATIEL (Association Technique de l'Industrie Européenne des Lubrifiants or European Lubricants Industry Technical Association), which also includes Group VI: Polyinternalolefins (PIO). In addition to the official classification, Group II+ is also commonly used in this field; this group includes saturated and sulfur-free base oils with viscosity indices greater than 110 but below 120. In these classifications, saturated hydrocarbons are paraffinic. It contains naphthenic compounds but not aromatics. There is also a definition for base oils (base stocks) according to API 1509: "A base stock is a mineral oil compound produced by a single manufacturer with the same technical specifications (regardless of the supply source or manufacturer's location), meeting the same manufacturer's specification, and identified by a unique formula, product designation number, or both. Base stocks are manufactured using very different processes." Base oil is the base stock or base stock mixture used in API licensed oil. Base stock types are 1) Mineral oil (paraffinic, naphthenic, aromatic), 2) Synthetic (polyalphaolefins, alkylated aromatics, diesters, polyol esters, polyalkylene glycols, phosphate esters, silicones), and 3) Vegetable oil. For a long time, the automotive industry in particular has needed mineral oils and, consequently, base oils with improved technical specifications. The technical specifications for the ultimate high-grade mineral oils increasingly require products with excellent low-temperature properties, the correct viscosity level, and low volatility. Generally, high-grade lubricating base oils are those with a kinematic viscosity of approximately 3 cSt or higher; a pour point (PP) of approximately -12 °C or less; and a viscosity index (VI) of approximately 120 or higher. In addition to a low pour point (PP), low-temperature fluidity of multi-grade engine oils is also required to ensure the engine runs smoothly under low-temperature conditions. Low-temperature fluidity has been demonstrated in cold Mars simulation (CCS) tests as apparent viscosity at -5 to -40 °C. Modern high-grade base oils with a KV100 of approximately 4 cSt should typically have a CCS viscosity lower than 1800 cP at -30 °C (CCS-30), and oils with a KV100 of approximately 5 cSt should have a CCS-30 lower than 2700 cP; the lower the value, the better. In general, lubricating base oils should have a Noack volatility no greater than that of currently available conventional Group I or Group II light neutral oils. Today, only a small fraction of the base oils produced can be used in formulations to meet the most current, demanding mineral oil specifications. It is no longer possible to produce mineral oils that meet the specifications of the most demanding automobile manufacturers from conventional mineral base oils (API Group 1, and in some cases Group 11). Typically, these oils contain very high concentrations of aromatic, sulfur, and nitrogen compounds, and also have high volatility and a low viscosity index. Furthermore, mineral oils generally respond moderately to antioxidant additives. Synthetic (PAO; API Group IV) and, as they are called, semi-synthetic base oils (VHVI; API Group III) are playing an increasingly important role, particularly in automotive mineral oils such as engine and gear oils. The service life of mineral oils is desirablely long, thus avoiding frequent oil changes by the user and also allowing for long maintenance intervals in vehicles, for example in commercial transportation. Over the past decade, engine oil change intervals for passenger cars have increased fivefold, reaching a maximum of 50,000 km. For heavy-duty vehicles, engine oil change intervals are currently around 100,000 km. A similar "longer life" development can be seen in industrial mineral oils. Synthetic PAO base oils are produced by oligomerizing alpha-olefin monomers, followed by hydrogenation to obtain a fully saturated paraffinic base oil. PAO base oils have relatively high VI values and also excellent low-temperature properties, with PP even below -60 °C. Due to proper product distillation, the products have low volatility and high flash points. The production and use of PAO base oils are quite limited due to the limited availability of the expensive raw material, namely alpha-oleons. Highly refined VHVI base oils are produced from crude oil by removing undesirable compounds. The most important step is the dewaxing process, which involves removing solid, long-chain paraffins or, using modern technology, converting these n-paraffins into liquid isoparaffins. GTL base oil is produced by the catalytic isomerization of synthetic FI wax. Compared to mineral oils, VHVI base oil products are more paragenic and have a narrower distillation range, therefore possessing a very high VI, lower volatility, and better low-temperature properties. These oils have extremely low aromatic content and are also essentially sulfur and nitrogen-free. In addition to the technical demands for vehicle engine technology, stringent environmental requirements are also driving the industry to develop more sophisticated base oils. Sulfur-free fuels and base oils are needed to achieve the full effect of new catalytic converter technologies in modern vehicles, reduce nitrous oxide, volatile hydrocarbon, and particulate emissions, and ensure the direct reduction of sulfur dioxide in exhaust gases. Traditional mineral oils contain sulfur, nitrogen, and aromatic compounds, and are typically more volatile, making them environmentally more harmful than the new sulfur-free base oils. Additionally, mineral oils are unsuitable for new engines with sensitive catalytic converter materials. The production of base oils is also being influenced by the increasingly widespread "Life Cycle Assessment" (LCA) approach. The aim of LCA is to assess the environmental burden of a product "from cradle to grave". LCA (Low-Calculation Analysis) is a tool for identifying the most critical points and making changes to extend the product's service life while minimizing environmental impacts related to its production, use, management, and disposal. Longer oil change intervals with high-quality base oils lead to reduced consumption of non-renewable crude oil and a decrease in the amount of hazardous waste oils. Currently, the use of recycled oils and renewable raw materials in the production of mineral oils is a frequent topic of interest. There is a desire to replace non-renewable fossil raw materials with bio-derived renewable raw materials in the production of hydrocarbon components, as fossil raw materials are exhaustible and have harmful greenhouse gas (GHG) effects on the environment. Problems associated with recycled oils include complex purification and reprocessing steps to obtain high-quality base oils. Furthermore, developing a functioning and comprehensive recycling logistics system is expensive. To date, esters have been the only renewable and biodegradable base oil type used in mineral oils. The use of these esters is limited to a few specialized applications such as chainsaw oils, bio-hydraulic oils, and metalworking oils. In normal automotive and industrial mineral oils, esters are mostly used as additives. High cost also limits ester use. In addition, esters used in engine oil formulations cannot be replaced with other esters without repeated expensive engine tests, even when the chemical composition of the substitute ester is essentially identical. Instead, base oils consisting of pure hydrocarbon structures can be partially interchanged. There are also some technical problems associated with esters. As polar compounds, esters tend to exhibit greater seal swelling than pure hydrocarbons. This has created a number of problems associated with elastomers in hydraulic applications. In addition, ester base oils hydrolyze more readily, producing acids that cause wear in lubrication systems. Furthermore, a major disadvantage of esters is that additives developed for non-polar hydrocarbon base oils are ineffective for polar ester base oils. FI 100248 presents a two-stage process in which the medium distillate is produced from vegetable oil by hydrogenation of carboxylic acids or triglycerides of vegetable oil to yield linear normal paraffins, followed by isomerization of the said n-paraffins to obtain branched paraffins. Hydrogenation was carried out at a temperature varying between 330 and 450 °C, under a pressure higher than 30 bar, and at a vacuum velocity of 0.5 to 5 liquids/hour (LHSV). The isomerization step is performed under high pressure. EP 774451 describes a process for the isomerization of fatty acids or fatty acid alkyl esters. Isomerization of unsaturated fatty acids or fatty acid alkyl esters is carried out using clay or another cationic catalyst. In addition to the main product, feedstock dimers are also obtained. After distillation, unsaturated branched fatty acids or fatty acid alkyl esters are obtained as products. GB 1 524 781 describes a process for the production of hydrocarbons from vegetable oil. In this process, the vegetable oil feed is pyrolyzed in three zones at temperatures of 300–700 °C in the presence of a catalyst. Gas, petrol, and diesel grade hydrocarbons are obtained in this process. These are separated and purified. EP 209997 describes a process for the production of base oils involving the isomerization of waxy hydrocarbons based on crude oil, resulting in only small amounts of light fractions. This process is used, for example, for the production of Group III base oils from bottom oils using waxy hydrogen. PAO processes are described in numerous patents. US Patent 6,703,356 describes a process using a large-pored crystalline catalyst in the production of PAO base oil from 1-alkene monomers, typically derived from crude oil-based ethylene. This patent describes the use of higher α-olefin monomers, preferably C14 to C18, instead of the typically used C10 (1-pattern) or C8-C12 α-olefin mixture as the starting material. Oligomerization of the α-olefins is followed by distillation of the product to the desired viscosity fractions, and hydrogenation to yield saturated "star-shaped" paraffins. It describes a base oil composition with a polycycloparaffin ratio above 15% and containing less than 0.3% by weight of aromatic compounds. The composition is obtained by hydroisomerization of isolated paraffinic wax obtained from the Fischer-Tropsch synthesis, followed by dewaxing and finally hydroprocessing. FI 66899 describes the use of fatty acid triglycerides and their polymers as base oils for mineral oils. The double and ester bonds of the final product are unstable due to oxidation and hydrolytic cracking. According to this publication, the base oils contain unsaturated esters. EP 03396078 presents a diesel fuel composition containing bio-components, which includes at least one component produced from a biological raw material of plant, animal or fish origin, crude oil-based diesel components and/or fractions obtained from the Fischer-Tropsch process, and optionally oxygen-containing components. The use of heteroatoms containing biologically derived starting materials for the production of high-quality saturated base oils or base oil components has not been reported to date. Based on the above teachings, it can be seen that there is an obvious need for a biologically derived base oil and a base oil component in which the oil in question contains branched saturated paraffins, and also that the highest quality requirements for base oils are met by considering the environmental impact, the impact on end-users, and the conservation of non-renewable raw materials, which is more favorable compared to conventional mineral base oils, and that the base oil in question technically surpasses existing products of the state of the art. Purpose of the Invention The present invention is described in the attached claims and requirements. One purpose of the invention is to provide a novel type of saturated base oil or a base oil component. Another objective of the invention is to provide a base oil or base oil component based on biologically derived raw materials, such as a base oil or base oil component that conforms to the quality requirements of API Group II+, preferably Group III base oils. A third objective of the invention is to provide a saturated base oil or base oil component based on biologically derived raw materials, such as an oil or component whose environmental, consumer, and non-renewable resource conservation impacts are more favorable than those of conventional crude oil-based base oils. The characteristic properties of the biologically derived base oil or base oil component, according to the invention, are presented in the annexed claims. Bulusuri general description: According to Bulusuri, a base oil or base oil component based on biologically derived raw materials contains saturated branched hydrocarbons with a carbon number range narrower than that of product distillates obtained primarily by conventional methods. The base oil or base oil component in question conforms to API Group II+, preferably Group 111 quality requirements. As used herein, the term "saturated hydrocarbon" refers to paraffinic and naphthenic compounds, not aromatics. Paraffinic compounds can be branched or linear. Naphthenic compounds are cyclic saturated hydrocarbons, i.e., cycloparaffins. Such a hydrocarbon with a cyclic structure is typically a derivative of cyclopentane or cyclohexane. A naphthenic compound may contain a single ring structure (mononaphthene), two isolated ring structures (isolated dynaphthene), two fused ring structures (fused dynaphthene), or three or more fused ring structures (polycyclic naphthenes or polynaphthenes). In this context, the term polyol refers to alcohols having two or more hydroxyl groups. In this context, the range of carbon numbers refers to the difference in carbon numbers between the largest and smallest molecules in the final product plus one. In this context, fatty acids refer to carboxylic acids of biological origin with a carbon number higher than C1. In this context, pressures are gauge pressures relative to normal atmospheric pressure. Detailed description of the discovery: Surprisingly, it has been found that saturated, high-quality base oil or base oil component containing branched saturated hydrocarbons with at least C18 carbon numbers and a narrow carbon number range can be produced from biologically derived starting materials, and these oils or components qualitatively correspond to API Group II+, preferably Group III base oils. According to the discovery, the distillation range (ASTM D 2887) of the biologically derived base oil or base oil component starts above 250 °C, the carbon number range and boiling point range are extremely narrow, and it also has an extremely high viscosity index and good low-temperature properties. According to the discovery, the biologically derived base oil or base oil component contains at least 90% saturated hydrocarbons by weight; The proportion of linear paraffins is less than 10% by weight. The range of carbon numbers of the base oil or base oil component of the invention is typically 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 carbon number is shown in dark color. 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 feedstock and also on the production process. In the structural examples in Table 2, the carbon number range of base oil components 1 and 2, produced by ketonization from a C16/C18 feed, is typically between C31 and C35, and the carbon number range of base oil component 3, produced by condensation from a C16/C18 feed, is typically between C32 and C36. Both represent the most common carbon number distribution of five carbon atoms. A feedstock containing a single 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 by the processes described below: 1. Isomerization of tallow fatty acid to obtain a branched product, followed by ketonization and finally hydrogenation. 2. Ketonization of palm oil fatty acid fraction, followed by hydrogenation and finally isomerization. 3. Condensation of palm oil C16 fatty acid distillate, followed by hydrogenation and finally isomerization. Structures of biologically derived base oils/components Base oil Carbon number %, by FIMS Structure 1 C31/ C33/ C35 acyclic component approx. 25% " ' " mononaphthenes approx. 50% ` .. . . . .. .. .. . Naphthenes approximately 25% › Structures of biologically derived base oils/components Base oil Carbon number %, by FIMS Structure 2 C31/ C33/ C35 acyclic component approximately 90% mononaphthenes approximately 10% r ' -' ~ i* 3 C3 2/ C34/ C36 acyclic component approximately 90% mononaphthenes approximately 10% Table 3 shows the carbon numbers and assumed typical structures of known synthetic hydrocarbon base oils of mineral base with similar viscosity levels. The carbon number range is determined by FIMS analysis. The structures of naphthenes are typical examples of a group of compounds. Typical structures of known base oils Base oil Carbon number %, Structure with FIMS 1 PAO C10 C30 approx. 80% + C4O approx. 20% Typical structures of known base oils Base oil Carbon number %, Structure with FIMS 2 FATTY WAX c25-c35 (FM) acyclic approx. 70% ' I" ' ' mononaphthenes approx. 25% dynaphthenes approx. 5% 3 VHVI C25-C35 mononaphthenes approx. 35% ll ' ., _ ~ ' l 'i C25-C35 dynaphthenes approx. other naphthenes approx. 10% i _ _ .V i ' 'i' The products in Table 3 are typically produced as follows: 1. PAO C10 is produced from 1-desden via oligomerization using a homogeneous catalyst. 2. YM is the isomerization product of the Oily Wax fraction of the mineral oil base. 3. VHVI is a hydrogen-fractured and isomerized base oil derived from mineral oil. Saturated hydrocarbons are classified according to carbon and hydrogen atoms using the FIMS method (field ionization mass spectrometry) as follows: 1 C(n).H(2n+2) paraffins 2 C(n).H(2n) mononaphthenes 3 C(n).H(Zn-Z) dynaphthenes 4 C(n).H(2n-4) trinaphthenes C(n).H(2n-6) tetranaphthenes 6 C(n).H(2n-8) pentanaphthenes. In Tables 2 and 3, percentages (according to FIMS) are given. 0/0) refers to the compound groups determined according to the method in question. Based on their molecular structures, the base oils or base oil components of the invention differ from the products of the known state of the art, as shown in Tables 2 and 3. The PAO base oil of the known state of the art mainly contains long (4-carbon) alkyl branches (structure 1 in Table 3). In the YM isomerization products of the known state of the art (structure 2 in Table 3), the short branches are typically at the ends of the hydrocarbon skeleton. The base oils or base oil components of the invention, shown as structures 2 and 3 in Table 2, are very similar to the YM base oils, but the YM base oil contains a significant amount of mononaphthene and also fused dynaphthene. When isomerization is carried out based on the double bonds of the fatty acid skeleton (structure 1 in Table 2), the hydrocarbon chain of the product is typically different. It contains 1 to 4 carbon alkyl branches. Branched compounds are mixtures of isomers that differ according to the branching regions. Branches in the hydrocarbon chain reduce the yield point significantly more than those at the ends of the chain. In addition to the position of the branches, their number also affects the yield point. The yield point decreases with increasing number of side chains, simultaneously causing a decrease in the viscosity index. In the products of the invention, a relatively high proportion of isomerized molecules contain more than 30 carbon atoms. Such high molecular weight compounds typically exhibit high VI, although the yield point (PP) is reduced to below -20 °C. As a result of the cleavage and hydrogenation of multilayered aromatic compounds, fused 3-5 rings (structure 3 in Table 3) are obtained in the state-of-the-art VHVI products. Polynaphthenes are also present, but not in the product of the current invention. Fused naphthenes make the PP-VI correlation weaker than alkyl branches. The best PP-VI correlation can be achieved with the optimal number of branches in the correct position. The product of the invention, obtained by isomerization of paraffin wax to hydrodeoxygen from ketone (structure 2 in Table 2), is a branched product with fewer methyl branches at the ends of the hydrocarbon chain and more methyl or ethyl branches within the hydrocarbon skeleton. The base oil in question typically contains some mononaphthenes, but not fused dinaphenes and polynaphthenes. These mononaphthenes are formed as a result of reactions of the double bonds of the fatty acid carbon chain or in isomerization reactions; therefore, according to their structure, they are obtained by hydrogenation of aromatics and cleavage of polynaphthenes in mineral oil. It differs from naphthenes. The product obtained by aldol condensation, alcohol condensation (Guerbet reaction), or condensation reaction by radical process contains a methyl dal in the middle of the main hydrocarbon chain (structure 3 in Table 2). The product differs from the VHVI and YM isomerization products of the known state of the art (structures 3 and 2 in Table 3), as the oils in question typically have branches at the ends of the chains. According to the discovery, the base oil or base oil component contains a product produced from biologically derived starting materials; this product contains less than 10% by weight, preferably less than 5% by weight, and especially preferably less than 1% by weight of linear paraffin; and at least 90% by weight, preferably at least 95% by weight, and especially preferably at least 1% by weight, as determined by gas chromatographic (GC) assay. The base oil contains 97%, and at best at least 99% by weight, saturated hydrocarbons. The product of the invention contains 5-50% mononaphthene with FIMS, preferably 5-30%, especially preferably 5-15%, and at best 5-10%; and less than 0.1% polynaphthene with FIMS as determined by the FIMS method. For the base oil or base oil component in question, the pour point (ASTM D 5950) is greater than, especially preferably greater than, 140 and at most greater than, 150, below -9 °C, preferably below -12 °C, and especially preferably below -15 °C. The low-temperature dynamic viscosity, i.e., CCS-point, as measured by ASTM D 5293, is less than -9 °C, preferably less than -12 °C, and especially preferably below -15 °C. -15 °C (ASTM D 5950). For the base oil or base oil component in question, the volatility of the product having a KV100 between 3 cSt and 8 cSt is determined by the DIN 51581-2 method (Noack method) at most. As determined by the FIMS method, the carbon number range of the base oils or base oil components of the invention is not more than 9 carbons, preferably not more than 7 carbons, especially preferably not more than 5 carbons and in the best case not more than 3 carbons. The distillation range of the base oils or base oil components of the invention is not more than 150 °C, preferably not more than 100 °C, especially preferably not more than 70 °C and in the best case not more than 50% by weight of the base oil. The distillation point is not more than °C (determined by ASTM D 2887 method with distillation points D10 and D90). The sulfur content of the base oil or base oil component is less than 300 ppm, preferably less than 50 ppm, especially less than 10 ppm, and in the best case less than 1 ppm, as determined by ASTM D 3120 method. The nitrogen content of the base oil or base oil component is less than 100 ppm, preferably less than 10 ppm, and especially less than 1 ppm, as determined by ASTM D 4629 method. The base oil or base oil component contains the carbon 14C isotope, which can be considered an indicator of the use of renewable raw materials. The typical 14C isotope content of the total carbon content in the product of entirely biological origin is at least (carbon 14C The 14C isotope content is determined based on the isotope content (ASTM D 6866). The 14C isotope content of the base oil corresponding to the invention is lower when other components, in addition to biological components, are used in the processing of the product, and is greater than 50%, preferably more than 90%, and especially preferably more than 99%. In this way, even low amounts of biologically derived base oil can be detected in other types of hydrocarbon base oils. The base oil or base oil component of the invention can be prepared from a feedstock derived from biologically derived starting material, referred to as biological starting material in this description. The biological starting material is selected from the following group: a) vegetable solid fats, oils, waxes; animal solid fats, oils, waxes; solid fish oils, fish oils, fish waxes, and b) vegetable solid fats, oils, waxes; animal fats, oils, waxes; solid fish oils, fish oils, fish waxes and fatty acids or free fatty acids obtained from their mixtures by hydrolysis, transesterification or pyrolysis; and c) vegetable fats, vegetable oils, vegetable waxes; animal fats, animal oils, animal waxes; solid fish oils, fish oils, fish waxes and esters obtained from their mixtures by transesterification; d) vegetable fats, vegetable oils, vegetable waxes; animal fats, animal oils, animal waxes; metal salts of fatty acids obtained from solid fish oils, fish oils, fish waxes and their mixtures by saponification; and e) vegetable fats, vegetable (f) oils, vegetable waxes; animal fats, animal oils, animal waxes; solid fish oils, fish oils, fish waxes and anhydrides of fatty acids derived from their mixtures, and (g) esters obtained by esterification of free fatty acids of vegetable, animal and fish origin with alcohols, and (g) vegetable fats, vegetable oils, vegetable waxes; animal fats, animal oils, animal waxes; fatty alcohols or aldehydes obtained as reduction products of fatty acids from solid fish oils, fish oils, fish waxes and their mixtures, and (h) recycled food-grade fats and oils and genetically engineered fats, oils and waxes, and (i) mixtures of the aforementioned starting materials. Biological Starting materials also include related compounds obtained 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, tallow 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 also animal fats such as lard, tallow and also waste and recycled food-grade solid and liquid oils and genetically modified oils. Solid fats, waxes, and oils produced through engineering are also suitable. In addition to solid and liquid fats, suitable starting materials of biological origin include animal waxes such as beeswax, Chinese wax (insect wax), shellac wax, and ianolin (wool wax), as well as plant waxes such as carnauba palm wax, ouricouri palm wax, jojoba wax, candeilla wax, esparto wax, Japanese wax, and rice bran oil. Biological starting materials may also contain free fatty acids and/or fatty acid esters and/or their metal salts or cross-linked products of the biological starting material. These metal salts are typically alkaline earth metals or alkali metal salts. The base oil or base oil component of the invention, which typically contains hydrocarbons with at least 18 carbons, is suitable if the carbon chain of the starting material molecules is at the level required for base oils (C18). They can be produced from biological starting materials by methods that result in extended processing. Suitable methods include processes based on condensation reactions, meaning reactions based on the functionality of feed molecules, in combination with at least one of the following: reduction, transesterification, hydrolysis, metathesis, decarboxylation, decarbonylation, isomerization, dewaxing, hydrogenation, and post-treatment or reaction. Condensation reactions include, for example, decarboxylate condensation (ketonization), aldol condensation, alcohol condensation (Guerbet reaction), and reactions involving dimerization, trimerization, oligomerization, and radical reactions in double bonds. Hydrocarbons, preferably saturated hydrocarbons, are obtained as products by processing biological starting materials, followed by fractionation of these hydrocarbons by distillation to obtain final products. In the ketonization reaction-based method, the acid groups of fatty acids interact with each other. They react to give ketones. Ketonization can also be carried out with fatty acid esters, fatty acid anhydrides, fatty alcohols, fatty aldehydes, natural waxes, and metal salts of fatty acids. The resulting ketone is reduced to give a paraffin, which is followed by isomerization to improve the low-temperature properties of the final product. Isomerization is optional when the branched feedstock is subjected to ketonization. In the ketonization stage, diol-containing dicarboxylic acids or polyols can be used as starting materials that allow for longer chain elongation than just fatty acids. In this case, a polyketonic molecule is obtained that will be processed similarly to a monoketone. In the ketonization reaction, the pressure is between 0 and 10 MPa, the temperature is between 10 and 500 °C, and supported by metal oxide catalysts. The catalyst used is preferably molybdenum, nickel-molybdenum, manganese, magnesium, calcium, or cadmium; silica and/or alumina can be used as support. Specifically, the metal in the metal oxide is preferably molybdenum, manganese, and/or magnesium in an unsupported catalyst. In the aldol condensation reaction, aldehydes and/or ketones are condensed to significantly increase the number of carbon atoms in the hydrocarbon flux. Saturated aldehydes are preferably used as feedstock. Branched unsaturated aldehydes or ketones are obtained in the process. The catalyst is preferably an alkali or an alkaline earth metal hydroxide, e.g., NaOH, KOH, or Ca(OH)2, with a temperature of 80 to 400 °C, preferably low temperature with low molecular weight feedstocks and high temperature with high molecular weight feedstocks. Temperature is used. The amount of catalyst to be used in a homogeneous reaction varies from 1% to 20% by weight, preferably from 1.5% to 19%. In alcohol condensation reactions, especially the Guerbet reaction, alcohols are condensed to greatly increase the number of carbon atoms in the hydrocarbon flux, thus obtaining branched monofunctional and branched multifunctional alcohols from monohydroxy and polyhydroxy alcohols, respectively, in the condensation reaction of alcohols. Saturated alcohols are preferably used as feedstock. Known catalysts for the Guerbet reaction, such as hydroxides and alkoxides of alkali and alkaline earth metals, or metal oxides in combination with a co-catalyst, can be used as reaction catalysts. The amount of catalyst to be used in the reaction varies from 1% to 20% by weight, preferably from 1.5% to 19%. Suitable co- Among the catalysts are chromium (III), manganese (II), iron (II), cobalt (II) or lead (II) or stannic oxide or zinc oxide salts; the salts are soluble in water or alcohols, preferably sulfates. Hydroxides of alkali metals are used as co-catalysts, with zinc oxide being the preferred component, at a weight of 0.05% to 1%. Chain extension by condensation reaction of alcohols is carried out at 200 to 300 °C, preferably 240 to 260 °C; the reaction is carried out under the vapor pressure provided by the alcohols in the reaction mixture. Water is released in the reaction; this water is continuously separated. In the radical reaction, the carbon chains of saturated carboxylic acids are extended with alpha olefins. In the radical reaction stage, 121 mol of Feedstocks containing saturated carboxylic acids and alpha olefins are reacted in the presence of a peroxyester, diacylperoxide, or peroxyketal catalyst, provided by the reaction mixture. Alkyl peroxides, such as ditertiary butyl peroxide catalysts, are preferably used. The amount of catalyst used in the reaction is preferably 1% to 20% by weight. In electrochemical synthesis, carboxylic acids, especially fatty acids in vegetable oils, are first extracted, followed by the formation of carboxylic acid salts by dissolving them in an electrolyte solution to neutralize the carboxylic acids for electrochemical oxidation. The salts are converted into long-chain hydrocarbons by a reaction known as the Kolbe synthesis. The carbon number of the resulting product is one carbon from that obtained using the ketonization reaction. It is lower. The reduction of the product obtained from the chain extension stage to hydrocarbons (paraffin) is carried out via hydrogenation, thus eliminating polarity due to oxygen atoms and also improving oxidation stability by saturating any double bonds. In hydrogenation, the product of the chain extension reaction and hydrogen gas are passed into a hydrogenation reactor at a pressure typically between 1 and 15 MPa and a temperature between 150 and 400 °C. In the hydrogenation stage, special catalysts containing Group VIII and/or VIA metals from the periodic element system can be used on a support. The hydrogenation catalyst is typically a Pd, Pt, Ru, Rh, Ni, NiMo, or CoMo catalyst supported by activated carbon, alumina, and/or silica. After the reduction process, although there is no ketonization of the unbranched feed components, other feed Methyl branched paraffinic wax is obtained from stocks. The low-temperature properties of the product can be improved by isomerization. In isomerization, linear hydrocarbons are converted into branched ones, thus liquidating solid paraffins. In isomerization, hydrogen gas and paraffinic components react in the presence of an isomerization catalyst. During the isomerization stage, the pressure is typically between 1 and 15 MPa, and the temperature is typically between 200 and 400 °C. Special catalysts containing a metal from Group VIII of the periodic element system, such as Ni, Pt, and Pd, and a molecular sieve can be used. Alumina and/or silica can act as supports. If branched structures are obtained from a chain extension reaction and the pour point of the product is sufficiently low, isomerization is not necessary. The above-described methods are used to produce products from biological starting materials. The products mainly consist of saturated hydrocarbons and their mixtures. Depending on the desired properties of the base oil, they can be used as base oils and their components in base oil production. The product obtained is a high-quality base oil or a base oil component belonging to API Group II+, preferably Group III, which is particularly suitable for the production of high-quality mineral oils, white oils, process oils, and oils for metalworking fluids. Advantages of the invention: The base oil or base oil component of the invention has superior technical properties compared to conventional hydrocarbon oils of the corresponding viscosity class. The narrow boiling point range indicates that the product does not contain any initial light fraction (meaning molecules significantly lighter than average), which is demonstrated by the reduced volatility of the product. This results in lower oil consumption and reduced emissions in practical applications. It provides this. There is no "tail" (meaning molecules significantly heavier than average) consisting of heavier components. This results in excellent low-temperature properties of the product. For the base oil or base oil component of the invention, the carbon number and boiling point range can be adjusted to the desired range by selecting the feedstock composition. For base oils of the known state of the art, the boiling point range is adjusted by distilling the product to obtain a fraction with the desired kinematic viscosity. It is preferable for mineral oils to contain base oils with narrow carbon number ranges and therefore narrow boiling point ranges. In this way, the base oil contains molecules of similar size that behave similarly under different conditions. The base oil or base oil component of the invention consists mainly of isomerized paraffins, the remainder being mononaphthenes and, to a lesser extent, unfused dynaphthenes. Mononaphthenic compounds, as well as unfused dynaphthenes, are known to have similar physical properties to isoparaffins. The fused naphthenes in the products, according to the state of the art, have lower VI and lower temperature viscosity properties, as well as lower oxidation stability. For the base oil or base oil component of the invention, the high VI of the product practically means that the amount of viscosity index improver VII, typically used in lubricating oil compositions, can be reduced. In general, for example in engine oils, component VII is known to be the main cause of deposits in the engine. In addition, reducing the amount of VII results in significant savings in formulation costs. Unlike conventional products derived from crude oil, the base oil or base oil component of the invention is free of sulfur, nitrogen, or aromatic compounds, thus allowing for safe use in applications where users are exposed to oil or oil vapor. Furthermore, the product of the invention has an excellent response to antioxidants and pour point depressants (PPDs), thus extending the service life of mineral oils prepared from this base oil and allowing their use at low temperatures. Compared to esters or other base oils containing heteroatoms, the base oil or base oil component of the invention is more stable to hydrolysis, meaning it will not readily decompose under humid conditions and release corrosive acids. The base oil of this invention is also chemically more stable than more reactive ester base oils and, furthermore, has increased oxidation resistance compared to ester base oil derived from biologically derived unsaturated fatty acids. Compared to esters, the non-polar base oil or base oil component of this invention is more compatible with conventional hydrocarbon base oil components derived from crude oil, base oil components obtained from the Fischer-Tropsch process, and also with mineral oil additives. In addition, there is no problem with sealing materials as is encountered with elastomers, for example with esters. The advantages of the base oil or base oil component of the invention include the fact that it complies with the base oil requirements according to API Group II+, preferably Group III, and can be used in automotive engine oil compositions like other base oils of the API classification, according to the same base oil substitution rules. The base oil or base oil component of the invention is derived from renewable natural resources, as can be determined from the 14C isotope content of the product. According to the invention, renewable biological raw materials make up an entirely new source of starting materials for high-quality saturated hydrocarbon base oil or base oil component. Furthermore, carbon dioxide emissions contributing to the greenhouse effect can be reduced by using renewable raw materials instead of non-renewable resources. The invention is now illustrated through the following examples, without intending to limit its scope. Examples 1 to 5 show long-chain paraffinic hydrocarbons produced from oxygen-containing biological starting materials via a ketonization-based process. The products are very suitable as base oils or base oil components without mixing limitations, and are also compatible with mineral oil additives. Example 6 shows the determination of the biologically derived base oil content in conventional mineral base oil. Table 4 shows the properties of the base oil components prepared from biological starting materials in Examples 1 to 5, and Table 5 shows the properties of the products under the known state of the art. Preparation of a hydrocarbon component from stearic acid fraction: A mixture of vegetable oils (linseed, soybean, sunflower, and rapeseed oil) was hydrolyzed, and the fatty acids were distilled to obtain product fractions according to their carbon numbers. The double bonds of the fatty acid fraction used as feed were selectively pre-hydrogenated. The resulting stearic acid fraction (C) was diluted with a biological feedstock-based paraffinic diesel fuel. The stearic acid content of the mixture was 31% by weight. The feedstock was ketonized in a continuous tube reactor using an MnO2 catalyst. The reactor temperature was 370 °C, and the WHSV was 3. 18-pentatriacontanone, i.e., stearone, was obtained as the product in a diluent. In the hydrogenation stage, the resulting stearone/diluent mixture was hydrogenated in a high-pressure Parr reactor using a dried and active NiMo Al2O3 catalyst to obtain linear paraffin. The ketone was hydrogenated at 330 °C under 5 MPa pressure at a mixing speed of 300 rpm until no ketone peak was found in the IR spectrum of a sample. It was hydrogenated in such a way as to result in stearic acid, resulting in linear C35 paraffin. The linear paraffin wax obtained from ketone was isomerized in a Parr reactor to obtain a branched paraffin from the base oil class using reduced Pt molecular sieve/Al2O3 as a catalyst. The preheated paraffin/diluent mixture obtained above was isomerized under a hydrogen pressure of 3 MPa and at 340 °C until -6 °C PP was obtained. Finally, the light fractions were distilled under vacuum, and then the paraffinic product was filtered via diatomaceous earth to complete the process. Preparation of a hydrocarbon component from fatty acids derived from palm oil: Palm oil was hydrolyzed and the double bond was selectively hydrogenated. Following hydrogenation, ketonization was performed. The solvent was removed by distillation. In the hydrogenation stage, the ketone mixture obtained above was hydrogenated in a Parr reactor using a dried and active NiMo/Al2O3 catalyst to give linear paraffin. The ketone mixture was hydrogenated at 3.3 MPa pressure and 340 °C with a mixing velocity of 300 rmp. Palm oil resulted in linear paraffin. The N-paraffin wax obtained from the ketone mixture by hydrogenation was isomerized in a Parr reactor at 340 °C under a hydrogen pressure of 3 MPa using a reduced Pt molecular sieve/Al2O3 catalyst until the PP point dropped below -15 °C to give a branched base oil viscosity grade paraffin. Finally, the light fractions were reduced. Distilled under pressure. Preparation of a hydrocarbon compound from fatty acid methyl esters: Purified animal fat was transesterified in two stages with methanol under alkaline conditions at 70 °C and 0.1 MPa pressure, thus obtaining fatty acid methyl esters. Sodium methoxide acted 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 biologically derived paraffinic diesel fuel. The fatty acid methyl ester content of the resulting feedstock was ketonized by weight. Thus, both saturated and unsaturated ketones were obtained as products. In the hydrogenation stage, the ketone mixture obtained above was processed into Sample Hydrogenation was performed in a Parr reactor as in Example 2. Isomerization was also carried out as in Example 2. Preparation of a hydrocarbon compound from isomerized fatty acids based on tall oil: A mixture of fatty acids from distilled tall oil was isomerized in a Parr reactor using a mordenite catalyst. H mordenite zeolite acted as a catalyst, and 3% water was used by weight of the total mass of the reaction mixture. The mixture was purged with nitrogen. The isomerization temperature was 280 °C, nitrogen pressure 2.0 MPa, and stirring speed 300 rpm. The catalyst was filtered, followed by distillation of the monomeric acids from the product under reduced pressure. The double bonds of the monomeric acids were separated using a Pd/C catalyst. The mixture was selectively hydrogenated in a Parr reactor using a specific method. Hydrogenation was carried out at 150 °C under a hydrogen pressure of 1.8 MPa. Linear fatty acids were removed from the mixture by adding twice the amount of hexane, then the mixture was cooled to -15 °C and the resulting crystals were filtered. Finally, the solvent was distilled from the isostearic acid fraction. The isostearic acid fraction was ketonized in a pipe reactor with a biologically derived paraffinic diesel fuel at a concentration of 30% by weight. The reactor temperature was 370 °C and the WHSV was 1.7. Thus, a mixture of isomerized ketones was obtained as a product. In the hydrogenation stage, this ketone mixture was hydrogenated in a Parr reactor as shown in Example 2. Solvents were distilled from the final product under reduced pressure. Then, n-paraffins were extracted from the product by solvent wax removal, and finally, the paraffinic product was completed by filtration via diatomaceous earth. The final product was primarily branched paraffins. Preparation of a hydrocarbon compound from tall oil-based isomerized fatty acids and dicarboxylic acid: The isostearic acid fraction prepared according to Example 4 and C6 dicarboxylic acid (adipic acid) were mixed in a 1:3 molar ratio. The feed mixture was ketonized in a Parr reactor using a MgO catalyst. The acid mixture was ketonized at 340 °C using a stirring speed of 300 rpm. In the hydrogenation stage, the ketone mixture obtained in this way was used in Example 4. Hydrogenated in a Parr reactor as in Example 1, and the light fractions were distilled under reduced pressure from the final product. Branched paraffins with longer chains than other examples were obtained as the product. Summary of Examples 1-5 Proceeding as in Examples 1-5, base oil components can also be produced from other vegetable, fish, animal or recycled food-grade solid fats and oils (e.g., frying oils) or from esters or soaps derived from the fatty acids of said solid fats and oils or from the corresponding alcohols and free fatty acids. Hydrocarbon components can similarly be produced from natural waxes composed of fatty acids and alcohols. On the other hand, the corresponding alcohols can be prepared from fatty acids, for example using a Ru/C catalyst, and the following can be obtained: The alcohols in question can traditionally be esterified with fatty acids. Thus, esters with a carbon number of C36 are obtained for ketonization, while natural waxes are typically C38-C46 esters. Preparation of a hydrocarbon compound from C16 alcohol derived from vegetable oil: For the condensation reaction, 200 g of C16 fatty alcohol, palladium chloride (5 ppm palladium), and 12 g of sodium methoxylate were weighed into a Parr reactor. Stirring was set to 250 rpm, temperature to 250 °C, and pressure to 0.5 MPa. Scavenging with mild nitrogen was continued to remove the water released in the reaction. The reaction was carried out until the amount of condensed alcohol was equilibrated in the GC analysis. After the reaction, the product was neutralized with hydrochloric acid, washed with water, and dried with calcium chloride. In the subsequent HDO step, the condensed alcohol obtained above was hydrogenated in a high-pressure Parr reactor using a dried and active NiMo/Al2O3 catalyst to give a methyl branched paraffin. The aldehyde was hydrodeoxygenated at 340 °C, under a pressure of 5 MPa, by stirring at 300 rpm until no alcohol peak was detected in the FTIR spectrum. The pour point of the methyl branched wax was 69 °C. The C32 paraffin wax obtained above was isomerized in a Parr reactor using a reduced Pt molecular sieve/Al2O3 catalyst to obtain a branched paraffin of the base oil class. Preheated paraffin was isomerized under a hydrogen pressure of 3 MPa and at 340 °C until a pour point 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 given in Table 3. Similar hydrocarbon compounds can be produced by other condensation reactions and similarly by radical reactions. The properties of the products produced are given in Examples 1-6. Analysis Ex 1 Ex 2 Ex 3 Ex 4 Ex 5 Ex 6 Method GC distillation ASTM D2887 (°/0 by weight) Molecular distribution (°/o by weight) Aromatics O 0 ASTM D2549 Paraffins 88 31 90.4 FIMS Mononaphthenes 12 49 9.2 FIMS Dynaphthenes 0 20 0,4 FIMS Other naphthenes 0 0 0 FIMS Sulfur, ppm <1 <1 ASTM D3120 / D 4294 Nitrogen, ppm <1 < 1 ASTM D4629 Properties of base oils in the state of the art Analysis API GpIII, HC- API GpIII, API API Method CDW HC-CDW GpIII, GpIV, D2270 Pour point -18 -12 -21 <-63 ASTM GC distillation ASTM GC-Noack, 13.3 5.8 12.5 DIN °/o by weight 51581-2 Molecular distribution, °/o by weight Aromatics 0.0 0.0 0.0 0.0 ASTM D2549 Properties of prior art base oils Analysis API GpIII, HC- API GpIII, API API Method CDW HC-CDW GpIII, GpIV, Dynaphthenes 16.1 20.3 3.5 0 FIMS Other naphthenes 9.8 13.6 0.2 0 FIMS Sulfur, ppm <0.2 <0.2 <1 ASTM D3120 / D 4294 Nitrogen, ppm < 1 < 1 < 1 ASTM D4629 HC-CDW = with hydrogen Preparation of a hydrocarbon compound from fatty acids derived from crushed, catalytically dewaxed base oil palm oil: Palm oil was hydrolyzed. Fatty acids derived from palm oil were used as feedstock following selective pre-hydrogenation of the double bonds of these fatty acids. The fatty acids were evaporated by nitrogen scavenging in a separate evaporator unit and ketonized continuously at atmospheric pressure in a tubular reactor using MnO2 as a catalyst. The reactor temperature is 380 °C, and the feedstock WHSV is 1 1/h-1. The C31, C33, C35 ketone mixture obtained from the ketonization stage was continuously hydrodeoxygenated in a tubular fixed-bed reactor using a dried and active NiMo/Al2O3 catalyst to give linear paraffins. Hydrodeoxygenation was carried out at 270 °C, under a pressure of 4 MPa (40 bar), and with 1 1/h WHSV. The linear paraffin wax obtained from the HDO stage was continuously isomerized in a tubular fixed-bed reactor using a reduced Pt molecular sieve/Al2O3 catalyst to give branched paraffins. Isomerization was carried out at 340 °C and under a hydrogen pressure of 4 MPa until the pour point of the product was below -15 °C. Finally, the lighter fractions were distilled and separated under reduced pressure. Hydrocarbon components can also be produced similarly from other vegetable oils, fish oils, and animal fats. Properties of the products in Example 7. Method Analysis Base oil 413 °C Base oil 356-413 °C ASTM D 5950 Pour Point ,°C -23 -32 ASTM D 5771 Fog Point ,°C -6.8 -24.7 CCS-35, mPas 2920 690 Properties of the products in Example 7. Method Analysis Base oil 413 °C Base oil 356-413 °C FIMS Paraffins 90.5 Mononaphthenes 9.5 Dynaphthenes 0 Other naphthenes 0 ASTM D 3120 S, mg/kg 0 0 ASTM D 4629 N, mg/kg 0 0 Determination of the biological origin of the hydrocarbon component The hydrocarbon component of biological origin was weighed as a Group III base oil based on mineral oil and thoroughly mixed. For the first sample, the base oil component of the hydrocarbon of biological origin was added; for the second sample, the base oil component of the hydrocarbon of biological origin was added. 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 in the atmosphere in 1950. Currently, the radioactive carbon content in the atmosphere is approximately 107%. The value 613C indicates a stable carbon isotope ratio of 13C/12C. This value allows for the correction of the isotope fraction in our process. Actual results are presented in the last column. Radioactive carbon content Sample 14C content, % Mineral oil 0.1 ± 0.07 Bio oil 106.7 ± 0.4 Mineral + bio, 5% by weight 5.0 ± 0.3 Mineral + bio, 10% by weight 10.8 ± 0.3 Carbon number distribution The ratio of the narrow carbon number distribution of the base oil product depends on the distillation. Figure 1 shows the carbon number distributions of VHVI. According to the invention, the carbon number distribution of the base oils is narrower than that of conventional base oils when similarly cut at 413 °C, corresponding to the distillation C26 paraffin. The base oils of the invention contain a higher amount of higher boiling fraction compared to the conventional product in the same viscosity range (KV100 approximately 4 cSt), as shown by the carbon number distributions in Figure 1. Carbon number -29.4 -28.9 -29.3 -26.9 Bio ratio, % 4.60 ± 0.28 .04 ± 0.29. Higher boiling compounds increase VI. DPalm oil ketonization of fatty acids El Stearic acid ketonization ÜC16 alcohol Condensation v-NMVLOONwOI Carbon number TR TR TR TR TR TR TR TR TR

Claims (3)

REQUESTS . It is a base oil, and its feature is that the base oil contains branched saturated hydrocarbons with a carbon number of at least C18, the total carbon content in the base oil is 14C isotope content, It must be at least 50% based on the radioactive carbon content in the atmosphere in 1950 according to ASTM D 6866, contain at least 90% saturated hydrocarbons by weight, less than 10% linear paraffin by weight, not more than 0.1% fused polynaphthene as determined by the FIMS method, 5-50% mononaphthene as determined by the FIMS method, and at least 50% saturated hydrocarbons by weight having a carbon number range width of not more than 9 carbons, and have a kinematic coefficient at 100 °C according to ASTM D445. 3-5373. . Base oil according to claim 1, characterized in that the 14C isotope content is more than 90%, preferably more than 99°. . Base oil according to claim 1 or 2, characterized in that it contains at least 75% by weight of saturated hydrocarbons, with a carbon number range width of not more than 9 carbons. . Base oil according to any one of claims 1-3, characterized in that the carbon number range width is not more than 7 carbons, preferably not more than 5 carbons and particularly preferably not more than 3 carbons. . Base oil according to any one of claims 1-4, characterized in that it contains at least 95% by weight of saturated hydrocarbons, preferably at least 97% and in the best case at least 99%. . Base oil according to any one of claims 1-5, characterized in that it contains less than 5% by weight and preferably less than 1% by weight of linear paraffin. . Base oil according to any one of claims 1-6, characterized in that it contains 5-30% and preferably 5-15% mononaphthene. . Base oil according to any one of claims 1-7, characterized in that it complies with the base oil requirements according to API Group III classification. . Base oil according to any one of claims 1-8, characterized in that said base oil is not excessive; its pour point is not higher than -9 °C, preferably not higher than -12 °C and particularly preferably not higher than -15 °C. 10. Base oil according to any one of claims 1-9, characterized in that the viscosity index of said base oil is higher than 115, preferably higher than 130, particularly preferably higher than 140 and best of all higher than 150. 11. Base oil according to any one of claims 1-10, characterized in that it is derived from starting material of biological origin selected from the group consisting of: a) vegetable fats, vegetable oils, vegetable waxes; animal fats, animal fats, animal waxes; solid fish oils, fish oils, fish waxes; b) vegetable fats, vegetable oils, vegetable waxes; animal fats, animal fats, animal waxes; solid fish oils, fish fats, fish waxes and their mixtures by hydrolysis, transesterification or pyrolysis, fatty acids or free fatty acids, and c) vegetable fats, vegetable oils, vegetable waxes; animal fats, animal fats, animal waxes; solid fish oils, fish oils, fish waxes and their mixtures by transesterification, esters, and d) vegetable fats, vegetable oils, vegetable waxes; animal fats, animal fats, animal waxes; solid fish oils, fish oils, fish waxes and their mixtures by saponification, metal salts of fatty acids, and e) vegetable fats, vegetable oils, vegetable waxes; animal fats, animal oils, animal waxes; fish oils, fish oils, fish waxes and mixtures thereof, anhydrides of fatty acids, and f) esters obtained by esterification of free fatty acids of vegetable, animal and fish origin with alcohols, and g) vegetable fats, vegetable oils, vegetable waxes; animal fats, animal oils, animal waxes; fish oils, fish oils, fish waxes and mixtures thereof, fatty alcohols or aldehydes obtained as reduction products of fatty acids, and h) recycled food grade fats and oils and genetically engineered fats, oils and waxes, and i) mixtures of the said starting materials. 12. Base oil according to any one of claims 1-11, characterized in that it contains less than 10% by weight of aromatic carbons, preferably less than 5% and particularly preferably less than 1%. 13. Base oil according to any one of claims 1-12, characterized in that the sulphur content is less than 300 ppm, preferably less than 50 ppm, particularly preferably less than 10 ppm and best case less than 1 ppm. 14. Base oil according to any one of claims 1-13, characterized in that the nitrogen content is less than 100 ppm, preferably less than 10 ppm and particularly preferably less than 1 ppm. 15. Base oil according to any one of claims 1 to 14, characterised in that the distillation range of said base oil is not more than 150 °C, preferably not more than 100 °C, particularly preferably not more than 70 °C and at best not more than 50 °C, wherein the distillation points are D10 and D90.