FI128144B - Process for producing a saturated hydrocarbon component - Google Patents

Abstract

The invention relates to a process for producing a saturated hydrocarbon-based high-grade base oil or base oil component. The process according to the invention comprises two main steps, which are oligomerization and deoxygenation. As feed, a biological feedstock containing unsaturated carboxylic acids and / or carboxylic acid esters is advantageously used.

Description

/ Sputtering is commonly used for lubricants found in rolling stock / stock;

777..7 /// -.- /. /. /> / sponge, / as white oils: and as metalworking fluids / Lubricants · Contains typical ///// '/ //:

essential oils and additional topics. For lubricant applications, 'the automotive industry /' / has long been demanding technical properties for lubricants, and hence base oils, as well as 'further' requirements for 'environmental and health' // // // in terms of effects have tightened. Conventional mineral oils will no longer be able to produce lubricants / lubricants according to the specifications of the most demanding manufacturer. Mineral oils often contain too high concentrations of aro- // / '/ ///; and sulfur and nitrogen compounds and have remarkable volatility and / / // '/// / / 7 / low viscosity index or viscosity-temperature dependence. / Also / /// 7 ^; // response of mineral oils mm. antioxidant additives are often weak./7 v - o

20055661 prh 02 -10-20199

Especially in automotive lubricants such as engine and gear oils synthetic and so-called. semi-synthetic base oils have become increasingly prominent. A similar trend can also be seen in industrial lubricants. ^ i The lubricant life is to be kept as long as possible so that the user does not i '? need to change oil very often and in order to eg. am Matti transport vehicles t / 'the longest possible intervals · Passenger cars · Motor oil intervals have increased by up to five times over the last ten years to 50,000 km. Heavy-duty vehicles now have engine oil change intervals of around 100,000 km. · - ':> /. hi /// D

High quality lubricants use base oils according to API (American Petroleum Institute) Group EI grade IV.APThe basic classification is given in Table L pk k y

Table 1, API Base Oil Classification

- Group

Satisfied jj Rikki '. j hydrocarbons i '' p-% '·!

pV '(XSTM D 1552 / D 2622 / _t (ASTM D 2O07) D 3120 / D 4294 / D4927) ~ t ··· y · xx; <90 and / or | / x> 0.03 /? ^ / • Viscosity7 · Index (VI) (ASTMD2270)

II • IV ϊχ

90and / or ?

X _ä! . . - · - ·>"

III

£ 90 <0.03 <VK 120 <VI <120> 120

Kai kki polyalfaolcfun it (PAO)

All other base oils not included in groups I to IV '; Group ΙΠ oils are very high'viscosity i index VHVI petroleum oils which are produced from crude oil by hydrocracking and then isomerizing waxy high-chain paraffins to branched 'paraffins. Group III oils include · also · mineral oil-based Slack Wax paraffins (SW-waxes) and Fischer-Tropsch synthesis such as coal or

20055661 prh 02 -10- 2019 ;;;;;;;; natural gas · wax oils (GTE wax-like isomeric shingle oils. Group TV oils are synthetic polyalphaffeins.

A similar classification is also used for ATlEE (Association of Technical Dept. Eurofeux Des Eubrifiants, Technical Association) of the European Lubricants Industry, but the ATIL classification is supplemented by Group VI: Polyethylene (PIO). In addition to the general 'official' classification, the industry also has a stupid 11¾, which includes a saturated and sulfur-free pem ^^ thi index greater than 110 but less than 120. Saturated hydrocarbons include para10 physical and naphthenic compounds, but not aromatics. '1'. '///.' '..'. '.

Manufacture of lubricants; generally influenced by the 1 Life Cycle and EHS (-Environment, Health and Safety) thinking that a product's life span must be minimized. Longer oil change intervals reduce the amount of non-renewable crude oil-based raw materials / consumables and the resulting waste oil, which is classified as hazardous waste.

The lubricants should be as / least harmful to the operators and the environment both during and after use./ This means low concentrations of base oils / In some cases. metals, aromatic compounds, easily / volatile components, and nitrogen and sulfur compounds. / / / /// - y '' 'ly <C Renewable Raw Materials and Recycled Oil; use in the manufacture of lubricants constantly raises increasing interest, the problem of 'recycled oils' is their difficulty in refining · and reprocessing them into high quality' bio-based lubricants, which refer to 'basic30' of biological raw materials, so far only esters are already limited to some ·· special applications like cold compressor oils, biohyd4

20055661 prh 02 -10-20199 ;;;;; y roller fluids and metalworking fluids. In NörmBleissa lubricants, they have been used mainly in the additive scale for industrial and industrial lubricants. <

t v The high price limits the use of esters · In addition, for example, in the automotive industry (oy) lubricant compositions, esters do not have any 7mm shifts, while other base oils have such. If the composition is moon-1 oy il o): permissible.the ester desire range argues, all expensive motor tests have to be carried out, although the replacement ester n list is basically chemically equivalent. Esters 'a y 1' u • have encountered some technical problems because the butter oils produced therefrom have a night-time nature: very much of the recycled base Esteli) riperukdjyjcn ustcnsidok> et are susceptible to hjdroh jullc producing witclujärjesklniv p) corroso. If the esters are made from unsaturated carboxylic acids, the ester linkages are very vulnerable at higher temperatures. The esters are remarkably polar and affect 7 l 'mm. elastomers used as sealing materials and hoses are completely different from non-polar or less polar base oils. This has been caused especially in high-pressure hydraulic applications such as biohydraulics 'y i y' 0 - t forestry machines. Another even more significant problem of esters is the development of existing polar compounds (less polar hydrocarbons (0--00 / - / ---- 7)); disappearance of additive effect in polar ester-based base oils ^^^ / y / / ί / οοy y 0 / - / yy /// / ') - - iy Biologic' hydrocarbon components, or bio-based raw materials, are used in the base oils target, / y; ;

o Because of the availability of renewable bio-based raw materials to replace fossil raw materials, their use is generally desirable. The aim is also to improve the utilization of bioperate y waste, such as livestock carcasses.) /))) :) o · y i / <-. y yyy y / y o yi o '- / - -1 -'. '77 -. y <- - 0 ---. .- 0, yy '-7 ----- 7-.' --y: / ''. y -'- '. ry-y ./o. y. y.) using a suitable metal bait peroxide initiator which is easily (7 y) t captured by hydrogen from the C-H bond, and the appropriate free shame is also effected by the oxygen in the air without heating the product.

20055661 prh 02 -10-20199, however, the reaction is slower. This cross-linking is based on Mole; oxygen-oxygen bonds. Crosslinking levels of triglycerides can be monitored by processing time and kinematic viscosity. The viscosity increases with time, and as the product decays, the viscosity increases with time. 'λ; '(kk;' 'ό kkk k- ^ kö

The thermal, non-bonded bonds are also reacted to prepare a stand oil (triglyceride) from which triglycerides are introduced into the reactor. Cross-silencing is an exothermic reaction, so keeping the temperature at 280 to 300 ° C requires both an effective heating to effect the reaction and an effective cooling to prevent the product from overheating.In addition, the reaction vessel must be cooled rapidly to achieve viscosity. V 'λ k' 'n) y {^ kk (;

k k - Published inIfCriyfAtivnért Encyclopedia tf Che ^^^

Dimer acids _and p. 768 are prepared from uninsulated carboxylic acids by radical reaction with a cationic catalyst at a reaction temperature of 23 ° C. In addition to the acyclic, branched, unsaturated dimeric end product, mono- and bicyclic dimers are formed. ; kk kk k kk 'j Unsaturated / alcohols may be oligomerically and optionally saturated 25 carboxylic acids with heat and / or catalyst The alcohol monomer is an acyclic, unsaturated, branched k 1 (1998) 159-169 describes the oligomerization of carboxylic acids, carboxylic acid methyl esters and synthetic alcohols and olefins into the corresponding dimers

20055661 prh 02 -10- 2019 ;;;;;; The above trig lys eride, carboxylic acid methyl ester, carboxylic acid diester and fatty alcohol dimer products can be used in lubricant applications, but as having heteroatom atoms have the same weaknesses as ester-based base oils. / y '/ ·? <· - - - '1 e' Prior Art-Known processes where 'the oxygen of a carboxylic acid or ester? 'shall be deleted. The decarboxylation of carboxylic acids yields hydrocarbons having one carbon less than the parent molecule. The applicability of the decarboxylation depends on the carboxylic acid used as the starting material. The most active are carboxylic acids having electron withdrawing substituents on the 1 / carbonyl carbon in the alpha or beta carbon. Of such compounds, carbon dioxide is readily cleaved when the temperature is increased because the ROCOH bond is weak.

Other types of fly-box discomfort with the opposite of hydrocarbon chain to carbon block are difficult.

Reaction Enhanced Catalyst, by Mäier, W. 'F. et al., Chemische ÄzzÄ / e (1982), 115 (2), 808-812 are prepared from carboxylic acids hydrocarbons -; - heterogeneous Ni / Al ₂ O ₃ and Pd / SiO 2 catalysts at a temperature of 180 ° C in a hydrogen atmosphere. The combined decarboxylation and hydrodeoxygenation of oxo compounds is; '- described by Laurent, E., Delmon, - Ra Applied Catalysis, As GarGrA

- (1994), 109 (1), 77-96 and 97-115, wherein the biomass-based pyrolysis oil was subjected to hydrodeoxygenation with sulfurized CoMoy-Al-O. and ΧίΜο γ-ALO, with catalysts at 260-300 ° C and 7 MPa hydrogen pressure. The hydrodeoxygenation step '; . the reactions are strongly exothermic and require high hydrogen. · '

FI 100248 discloses a two-step process for the preparation of vegetable oil from middle distillation by hydrogenation of the vegetable oil carboxylic acids to different di t straight-chain n-j normal paraffins and isomerization of the n-paraffins to branched paraffins. Hydrogen treatment was carried out at a temperature of 330-450 ° C, about 3 ° C.

MPa pressure and fluid flow rate LHSV 0.5 - 5 1 / h. In the isomerization step 30, a temperature of 200-500 ° C, an excess pressure and a fluid flow rate of LHSV / µ 0.1 to 101 / h were used. y / //? 0 -2 / 7

20055661 prh 02 -10-20199

Methods are also known for the preparation of diesel grade saturated hydrocarbon components from organic oils by hydrogenation processes with NiMo and CoMo catalysts at 350-450 ° C. <7 yy y: T y -y y y Precious metal catalysts are used in isomerization processes which are: t · y expensive and very sensitive to catalyst poisons and vedclley Bio-based raw materials contain a large amount of oxygen which, when processed, produces · vet-i y? carbon monoxide and carbon dioxide. In addition, bio-derived feedstock contains nitrogen, sulfur and phosphate compounds which are known catalyst poisons and inhibitors of noble metal catalysts. These will reduce the life of the catalyst and will require frequent regeneration of the catalysts, unless removed prior to the isomerization process. ' i? i yyy '· yy · y · - 1 / y Triesters of vegetable oils, animal fats and' fish oil 'containing typically glycerol fatty acids15 as shown below

yy y where R ₁ , R 4 and R 4 are C 4 -C 30 hydrocarbon chains Fatty acids are hydrocarbons: straight-chained and long-chain carboxylic acids. The main hydrocarbon chain length is 18 carbons (Cl 8) 7 Cl 8 Fatty acids are typically bonded to the middle. The fatty acids associated with the other two hydroxy / l moieties have a typical carbon number in the panel and the carbon number in the C14-C22Wal. y - 7 y

The fatty acid composition can vary enormously in non-originating fats and oils. Although fatty acids may have multiple double bonds, they are not '' conjugated, but have at least one -Chy unit in between. Con fi guration Haan

20055661 prh 02 -10- 2019 ;;;;;; / natural fatty acid hinge bonds are in the cA form, where the hydrogen is on the same side of the rigid double bond. as the number of double bonds increases, the amount of doxicin depends on where the vegetable or animal fat or wax comes from. Animal fats typically contain ·· more saturated fatty acids than double-bonded fatty acids. Fatty acids in fish oils are rich in 'pearls' and have a longer average hydrocarbon chain; like vegetable oils and animal fats. The fatty acid composition plays a role in the assessment of the oxidation resistance, heat resistance, cold performance, and type of oligomerized products that are fed to the oligomeric parent.

Waxes are mainly carboxylic acids esterified with long chain alcohols. In addition, the waxes contain various amounts of the originating finins (n-alkanes), ketones and diketones, primary and secondary alcohols, aldehydes, alkanoic acids; 15; (carboxylic acids) and terpenes. The carbon number of these carboxylic acid and carbon black chains is typically C12-C38. 7 7 7 7 ..70x77 77777.7 7 '·' 77L N7y v Raw materials of biological origin are generally pretreated by suitable known methods • such as thermally, mechanically, for example, by shear, kernially, e.g. by acid or alkali, or by physical irradiation, distillation, &gt; 7 < by cooling or Filtration prior to processing, the chemical and physical pretreatment is intended to remove taf 'stunning impurities that impede the processing and to minimize unwanted side reactions. Feed impurities are generally compounds containing heteroatoms which are catalyst poisons. Impurities can also be components of product degradation resulting from processing, such as aromatics. 7 '·; · / In hydrolysis processing Oils and fats react with water to form a product

Industrial processes for hydrolysis of fatty acids307 7 are known mainly for three processes: high-pressure triglyceride vapor deposition, alkaline hydrolysis and enzymatic hydro9

20055661 prh 02-10-209 // //: lysis / · In a typical steam sputtering process, the hydrolysis of triglycerides by means of a curl is achieved at a temperature of 250 to 260 ° C and a pressure of 4 to 5.5 MPa. catalyst

S / Z may be added to accelerate the reaction. High temperature and headband / help dissolve grease in water. //; // :: / 1 // / 5 / / / ·: / / / / j ·: 1 //: 1 / / /: / o Paraffinic synthetic base oil components prepared by oligomerisation are known in the art, the most typical of which are PAO Qmlyalpha olefi (polym These are based on: · Non-Heterogenous Crude Oil Starting Materials Polyalfaole10: Phine-type base oils began to develop in the 1930s in both the USA and Germany, where products with good cold properties were mainly used for airplanes. Commercially available PA8fis utilizes C8-C12 alpha olefins or C14-C18 alpha olefins as the raw material, PAOm in the manufacture of monomer is thermally polymerized to a heavier Ziegler type: or. With the aid of Cräfts type catalysts or zeolite catalysts:: distilled to the desired product fractions and hydrogenated The saturated parafiineik: ·: SIL-PAO products may be prepared by the encirclement of viscosity grades, which tyypillisim / low viscosities at a temperature of 100 ° C (ADT 00) are 2, 4, 6 and 8 mm ² / s. In addition, extra thick base oils PAÖ40 and PA0100 with a KP100 value of: 40 and: i00 mm ² / s are produced and commonly used for thick lubricants:

/ fabrication and viscosity index (VII) viscosity index; im // proverk / high viscosity index of the PAO product line and at the same time excellent'kyI->

/ <In addition, the melting point, even at -60 ° C. From product merit / PIs are prepared by oligomerization of internal olefins in which the double bond is not at the end of the / oligomerizable olefin, as in alpha-o-lefines, but: distributed statistics30 Because of this, pimudale of the entire hydrocarbon chain. Internal olefins can be prepared by: dehydro / gelling crude oil-based n-paraffins. Internal C 5 -C 16 linear olefin 10

20055661 prh 02 -10-20199 The molecular structure of the products made from them differs from that of PAO. The properties of P10m compared to PAO have a lower viscosity index, a lower pour point and a higher volatility: are qualitatively located between PAO and VHVL. PlOm's production technology is similar to that of PÄO, but the oil-less PAO and PlOrö of less reactive internal olefins are relatively poor due to the lack of polarity. To improve solubility, the formulations are often used in esters

The use of a heteroatom-containing organic feedstock or intermediate, optionally thermally and / or chemically and / or physically and / or mechanically treated, has not been reproduced in the process of attenuating a high quality saturated base oil or p component. y

1-5 In view of the foregoing, it can be seen that there is an obvious need for a new Alternative process for the preparation of the hydrocarbon component, preferably from bio-based raw materials, by which the process can

Significantly reduces the level of technology _: Tannettian solutions: problems. In addition, there is a need for a polytonic saturated base oil that meets the quality requirements of a base level oil that is preferably of biological origin and has the advantage of: λ similar effects on environmental and end-user karma than on traditional mineral oils. 'In addition, there is a need for a process 1 le based on non-renewable'': raw material conservation and renewable raw material utilization.

BACKGROUND OF THE INVENTION An object of the invention is to provide a process for the preparation of a saturated hydrocarbon component which preferably utilizes organic raw materials.

It is also an object of the invention to provide a process for producing a base oil or base oil component ό: 0. '/ <: <λ ό:: s <:; :;

σ> ο

C \ J ό

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Another object of the invention is to provide a process for the preparation of a saturated base oil or base oil component containing no heteroatoms from organic raw materials. <ύ? - '>' 'Ϊ:' '' '

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It is also an object of the invention to provide a process for the preparation of a non-heteroatom-saturated diesel component, Jia Fensin Component, from bio-based raw materials. (O '?' /; 'Λ';

It is also an object of the invention to provide a base oil or base oil component which fills

API Group III requirements. / '' ('/' '(·' Q? · / Ό · /) The characteristic features of the process according to the invention and of the base oil are shown.

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CM; Invention ^{: The} prose comprises an oligomerization step in which the feedstock molecules react with each other to increase the carbon number of the resulting component, and a deoxygenation step. Deoxygenation can be accomplished either by hydrodeox20 synthesis reaction or by decarboxylation / decarbonylation reactions. The process of the invention may further comprise an optional isomerization gap for isomerization of lighter products and / or a finishing step. Preferably · organic feedstock is used as the main feed. lv

Ö1 Igomerization herein refers to dimerization, trimerization, and tetramerization reactions, as well as dust dimerization and crosslinking reactions. p o p? d g p t;

The oligomerization step of the process according to the invention is carried out to increase the hydrocarbon chains of unsaturated carboxylic acids and / or their derivatives such as · esters, anhydrides and alcohols from monomer units to dimers of two monomer units and larger oligomers. Here is oligome12

20055661 prh 02 -10-20199 In the toe reaction, the double bonds of the compounds react with one another under the influence of heat and / or catalyst. / 7 7 ^^^^^ 7 7/17 / O / Carboxylic acid and their derivatives. The carbon number of carboxylic acids and their derivatives is women. 77 7 7 7; 7,777 / 777,777 / 7,7,4 ^ 4 ^ rDeoxygeneration is meant herein to mean the removal of oxygen by either hydrodeoxyoxygenation or reaction by complete decarboxylation / decarboxylation reactions. After deoxygenation, the structure of the 77 7 biological feedstock has changed to either paraffin or olefin 7 depending on the catalyst and reaction conditions. 7 7 // - 7 // 77;

Hydro means: · the removal of oxygen by hydrogen.

Water is released in the reaction. In this case, the structure containing the ester, alcohol, anhydride or carboxylic acid groups is decomposed and the potential oxygen, nitrogen, phosphorus and sulfur compounds are removed as well as the light hydrocarbons as gases. Decarboxylation herein refers to the removal of carboxylic acid as carbon dioxide and decarbonylation refers to the removal of carboxylic acid as carbon monoxide.

Isomerization, as used herein, refers to the isomerization of straight chain paraffins which delivers branching structures. 77 77 7: T

In this context, saturated hydrocarbons include paraffinic and naphthenic compounds, but not aromatics. Paraffinic compounds may be either branched lice:

? : straight chain.7 Naphthenic compounds are Cyclic-saturated hydrocarbons or 'cyclic;

\ 7 loafing. Such a ring-structured hydrocarbon is typically a derivative of pulseOpentane or cyclohexane. In naphthenic compound, loose · one filler30 amp ring structure. 7 77 7 7 7 77 7 7 70 7 7 7/7; 7 σ> o

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CM? The saturated base oil herein comprises saturated hydrocarbons.

/: The pressures here are overpressures relative to normal atmospheric pressure:

/ 5/77/7 · / <· 7 7 The classification of a periodic rigid system is the IUPAC classification./ 7

The carbon number range as used herein refers to the difference between the highest and lowest molar / carbon numbers plus one. 71 7 77 7 7 7 7 7 7 7 77777 io7 //. 1/7 ti7 77777 / -7 / 7/7

The invention is illustrated by the following Figure 1, however, the embodiment is not intended to be limited thereto.

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CD mmoo CM / FIGURE: / 7 71 1,177 - / <lkl / 7 T // 'Ilii // l <77: <71t': 'q / .17: 7 // <7 / 11'77' · ' // '! Figure 1 illustrates a preferred embodiment of the process according to the invention for process / 7 '. One or more feeds selected from: triglyceride feed stream 1, fatty acid feed stream 2, ester feed stream of fatty acids and short alcohols, Sp. recycle product fraction (eg 52) or hydrocarbon stream 201. Dilator current. 202 1 / comprises a mixture of circulating stream 52 or hydrocarbon stream 201. From Oligomeric Reactor 10, a product 11 containing feedstock reactants reacted with its prodrug bonds and hydrogen as a stream 7 to an optional prehydrogenation reactor 20 is provided, where 77 optionally a diluent stream 202 can be fed. - The product obtained from its prehydrogenated reactor 120 is hydrogenated 21

Optionally, a diluent 202 may be introduced into the 7 / deoxygenation reactor.

the gas stream uses a mixture of hydrogen -7 and incert gas such as nitrogen (not shown in Chapter 7). Containing saturated hydrocarbons from deoxygenation reactor 30

20055661 prh 02 -10-20199 the product is conducted in a stream 31 to a distillation and / or separation part40, where the different product fractions gas 44, gasoline 43, diesel 42 and base oil 41 are separated. Optionally, the lower fractions of gasoline 43 and diesel 42 are isomerized in a hydrofluorocarbon unit 50 in the presence of hydrogen 7 to provide streams of gasoline 51 and diesel 52 containing branched hydrocarbons. in particular fatty acids 2 or fatty acid esters 3 and / or fatty alcohols 6; the oligomerized components are recycled to the oligomerization reactor 10 in a stream, and the oligomerized components are introduced into the pr

80 wherein the saturated components 81 are separated from the double bonded components 82 leading to the oligomerization 10. a post-oligomer &apos; in-70 which can be supplemented with lower molecular weight 1 / unsaturated carboxylic acids 8 or olefins 5 to form straight chain 'non-oligomerized' unsaturated components. Post-oligomer-reactive feeds are fed as a stream 71 to an optional pre-hydrogenation reactor 20. lit <

'i--' i-2 - <

DETAILED DESCRIPTION OF THE INVENTION Surprisingly, it has been found that the process of the invention comprising an oligo? fatty acid esters and fatty acid esters: 'high grade fatty oil or base oil component. Problems with prior art processes and the products made with them can be avoided or at least avoided. The process of the invention can be substantially reduced. 1 '' / ·,; - p 1 • · /

In particular, the process of the invention can utilize oligomerization reactions of bio-based materials in combination with a co-ooxygenation reaction from the production of a saturated base oil in a novel way. Unsaturated carboxylic acids and / or derivatives thereof such as fatty acids, fatty acid esters, fatty alcohols, fatty acid anhydrides or mixtures thereof are oligomerized from monomer units to dimers of two lumps and larger. When using bio-based raw materials in the production of base oil, it is necessary to increase the length of their hydrocarbon chain to the base carbon number of base oil oils such that no non-carbon-carbon bonds are distributed in the basic structure of the molecule. According to the invention, this is accomplished by reacting the double bonded compounds to form the desired carbon-carbon bonds in the molecules and causing the hydrocarbon stream to have a carbon number increase in the range C18-C55O. Typically, the base oil applications have a carbon number range of Cl 8 to 076 and particularly thick base oils can have a carbon number range up to Cl 50 to C550. For example, in the oligomeric reaction, the double bonds of the triglycerides react with each other to form a polymeric triglyceride network. Other feeders provide dimers and trimers and tetramers formed mainly through double bonds. If the feed contains polyunsaturated hydrocarbon chains, - after Oligomer o Inn and deoxygenation - more trimeric and ring hydrocarbons are produced compared to monounsaturated hydrocarbon chains.

In the process of the invention, the feed of biological and / or synthetic origin is oligomerized and deoxygenated. Preferably, the oligomerization of the unsaturated feeds is first performed and then the resulting product is subjected to deoxygenation to remove the heteroatoms to yield the saturated paraffins. Alternatively, the unsaturated feed is first deoxygenated to remove the heteroatoms and then oligomerized to the olefinic product thus obtained, however, the deoxygenation is carried out by a decarboxylation or decarbonylation reaction and is not suitable for the hydrodeoxygenation reaction.

20055661 PRH 02 -10-20199

The process may further comprise an optional lighter component after isoforms deoxygenation. Short chain non-basic petroleum paraffins formed as by-products of the process can be large-sized to form hydrocarbon-containing side branches in their hydrocarbon chain. These isomerized products can be used, for example, as petrol or diesel components, and the C18-C24 carbon components can also be used as light pumice oil components; i '/ 7 -7777 - 7 / - 7

The process may further comprise: a selection of precursor hydrogenation or ethhetideoxygenation, an optional residual oligomerization step, an actual oligomerization step, optional intermediate purification steps, product recycling steps and a finishing step. The feed may be subjected to one or more pre-treatment steps to purify and / or prepare the feed. ''

1 (SUPPLY In the inventive process, the feed comprises one or more components selected from the esters of triglycerides, C4-C38 carboxylic acids, C4y C38 carboxylic acids and C1-C10 alcohol alcohols, C4-C38 carboxylic acid and Preferably the feed is selected from trig '-' lyserides, esters of C4 to C24 carbonates, esters of C12 to C24 fatty acids and C1 to C3 alcohols, C12 to C24 fatty anhydrides, C1 to C24 fatty alcohols, and mixtures of the foregoing. ^^^ bio-based raw material or mixtures thereof, -; 25 // · '·' 't · <i - /' · / 707 y

7 Suitable bio-based raw materials are selected from the group consisting of 7 7 7 '7 77

77 7 (a) Vegetable fats, oils, waxes, animal fats, oils, waxes and hand fats, oils, waxes, and 0 7 7 ^^^^^ 7

7 (b) vegetable fats, oils, waxes, animal fats, oils, waxes, fish17

20055661 prh 02 -10-20199 '' '' '1'1' 'of free carboxylic acids, and 1 11 1 1 <

'11' '' '11' (c) The esterification of hand fats ,: -Oils, waxes, animal fats, oils, waxes, fish 77: ^: 7 ^ oils, waxes and the like, by '5n' 1 esters, and 11 1 1 1 1117 .λ7 lv1; .- 7; i '·, j. 7 '.

1 '·' d) esters obtained by esterification from free carboxylic acids of vegetable, animal and fish origin with alcohols 1 1 '1, and' 7: -17 ejv vegetable fats, 7-oils, l-waxes, non-fatty oils, and fatty alcohols obtained as reduction products, i · i · f) recycled edible fats and oils, genetic manipulation 11a ready 11 7 prepared fats, waxes and oils, and

In this context, plants include algae and animals include insects. The bio'1-derived raw material may contain free carboxylic acids or carboxylic acid esters or oligomerization products of the biological raw amine, from which they are substantially processed. All feed types mentioned above, which are made wholly or partly synthetically, are also suitable for feed. '' 71 11 20 --- 15 '' Since the process / purposes are on-line / double bond / feed circuit components, it is preferable that the feed contains at least 50 wt.% and preferably at least 80 wt.% of unsaturated and / or polyunsaturated compounds.

Preferably, the unsaturated compound is a non-mono-unsaturated component, particularly preferably a '25 L Cl 6: 1 and / or 018: 1 component having a content of the feed mixture greater than 40% by weight and;

preferably more than 70% by weight. : '' 1 1 11 <j 7 '' '1 .. .1. .7 '1. 7.' '. . 1 11 '.

Suitable Biological Raw Materials Fish Oils such as Ground Oil, Herring Oil, Tuna Oil, Anchovy Oil, Sardine Oil and Mackerel Oil, Vegetable Oils

- - such as rapeseed oil, rapeseed oil, canola oil, tall oil, sunflower oil, soybean oil, corn oil, hemp oil, olive oil, linseed oil, mustard oil, palm oil,

20055661 PRH 02 -10- 2019 / walnut oil, castor oil and coconut oil, animal fats such as lard, tallow and trawl and edible fats and oils. Other suitable bio-based raw materials include fats made from GIF, low and Oils, and waxes of animal origin,

- such as beeswax, Chinese wax (insect wax), shellac wax and lanolin (wool: 5 ha) as well as herbal waxes such as Carnauba palm wax, Ouricouri palm wax, <'· jojobao Ijy, sturgeon wax, esparto wax, and Japanese rice wax. Also suitable are unsaturated alcohols found in nature, such as alcohols with natural waxes and branched alcohols, t 1 · '

The process may also be used to process mixtures of organic and synthetic feedstocks, where appropriate, as feedstocks, other feedstocks or synthetically prepared feedstocks suitable for the particular process step may be used. Also cleaner: S-inset: Inputs Are edible, although the products are then not subject to renewable abrasion <

i ·? i yy / yy: yyyyyyy yy

If desired, straight-chain and ring-rocket olefins, preferably C2-C14 olefins, may also be added to the feed, whereupon the product will be grown at lower carbon numbers than the typical C12-C24 carbon number range. Suitable olefinic additional components may be 20 pine essential oils, such as alpha-pineeh and / or double bond compounds prepared from sugars t and / or unsaturated compounds and / or synthetic compounds prepared from carboxylic acids by metathesis. o k 1 / y ...: p \? y y y y y y y

Shorter y '(< C12) unsaturated dicarboxylic acids, carboxylic acids, alcohols, and alkyl esters may also be utilized as additional feeds in oligomerization, whereby the molecular weight of the product may also be increased with lower carbon numbers. Suitable · unsaturated dicarboxylic acids include, for example, tnaleic acid, fumaric acid, citric acid, mesaconic acid,

20055661 PRH 02 -10-20199 ///// ;;;;;; / / In the optional post-oligomerization reaction of the invention, double-bonded to a carboxylic acid or an alkyl ester of a carboxylic acid or a triglyceride

Or other double bonded molecule may be oligomerized, for example, with the above short hydrocarbon molecules /

7.5 / the compounds of the base compounds are mainly in the middle of the high chain, the smaller molecules are reacted to the deoxygenation step; ? 1 phine molecule, · 7,177 / p? t y; p // y s t 7: / 71

Because of the short lifetime of the catalyst in the processing of carboxylic acids, the feed can be converted to less aggressive catalysts · or 'alcohols, the various triglycerides can be converted to the alkyl esters 7, whereby the triglycerides decompose with the carboxylic acid. ester and triglyceride alcohol moiety or glycerol Release / Alcohol:

7 methanol is typically used, but other 7 & alpha &gt; C 1 -C 10 alcohols may also be used. Typical transesterification conditions are as follows: temperature 60 to 70 ° C and pressure 0.1 to 2 ^: MPa, .CatalystFor use of sodium and potassium hydroxides7

7 dissolved in excess methanol / The esterification of free carboxylic acids and alcohol requires higher temperature and pressure (e.g. 240 ° C and 9 MPa or H 2 O). 77/7 7 7 7 7 / / 7/7 7 7 - ../ 7.7:

The carboxylic acids can also be reduced in known ways to fatty alcohols, either directly by reduction of the acid groups to alcohols with lithium aluminum hydride, whereby double bonds remain in the alcohol, by hydrogenation of the al 25

At 230 ° C and 20-30 MPa hydrogen pressure. In the hydrogenation reaction, the alcohol moiety used to esterify the carboxylic meat is released and can be recycled

7; esterification and unsaturated fatty alcohols are led to oligomerization. '/

20055661 prh 02 -10-2019 '' '' '':: For optional feeds ·· and · diluent / in various process steps: can be added: hydrocarbon, eg diesel-grade biocarbon. The diesel-grade hydrocarbon boils at a sturgeon at 150 -400 ° C, typically 1 ^ -7: // 1 • 57 7 Preferably, the feedstock-derived feedstock is pretreated and / or prepared by methods known in the art, e.g. impurity-depleted 7/7 The hydrolysis reaction of triglycerides can be utilized to prepare carboxylic acids to be used as the oligomeromeric feed. The compounds can be hydrolyzed after oligomerization. Hydrolysis yields glycerol as the catalyst, and thus no hydrogen is consumed in the HDO step to hydrogenate the glycerol to propane gas. By distillation, for example, either the cyanide may be added; / to fractions of a lower humidity or carbon number, by filtration through a suitable 'filter aid' · impurities in the feed or in the final product can be removed:

151 // PROCESS: / · 7 /// p7 //

According to a preferred embodiment of the process of the invention, the olefin feed is comprised of two-linked triglyceride carboxylic acid, anhydride or fatty alcohol components. The feed contains at least 50 to 20% unsaturated and / or unsaturated compound. For the preferred feed step, one of the feedstock coefficients is selected as the main feed and the oligomerization ratio ratios are adjusted according to the main feed. Other inputs may be mixed with the MAIN INPUT insofar as they do not adversely affect the prOSeSSOM ^ s advantage of processing. 7 // y 7 // / ^^^^^ / · / · - ^: - 4/31/7 / ^ 74 ^^ - // 7-7 - / - ^ / 1: 1 - //// The oligomerization reactions are catalyzed by heat and a suitable catalyst. Suitable cat 7 lytes are cationic clay catalysts, preferably zeolite catalysts and particularly preferably morphormorillonite. Additional reagents such as water can promote the oligomerization reaction of the carboxylic acids. For carboxylic acid feed, up to 10 wt%, preferably 0.1 to 4 wt%, and most preferably 1 to 2 wt%. No water: excess use is recommended,

20055661 prh 02 -10-20199; '- this is when the byproducts of the non-dimerized blocking bonds start to form as a by-product •' / 'carbon-carbon bonds. 1 't' '? Suitable oligomerization reactors include, for example, a fixed bed reactor and a stirred tank reactor. Reaction solvents may be used in the reaction to adjust the oligomer distribution. A suitable recyclable die or other hydrocarbon from the lam process. Typically, the pressure of the oligomerization step is from 0 to 10 M at a temperature of 100 to 500 Ύ1, preferably with a batch reaction of 0.01 to 30% by weight of the total reaction mixture, preferably 0.5 to 10% by weight. When using a fixed bed reactor, the feed amount in grams per milliliter of catalyst is preferably less than 4 hours. By using a short residence time, the lighter, 'non-oligomerized' components can be separated from the heavier already oligomerized t components, for example by distillation, and subsequently recycled into the oligomerome. Saturated components are led to deoxygenation and superficial isomerization to branch their hydrocarbon chains.

· Hydrogenation catalysts lose their activity mainly in the form of a coke wax formed on the surface of the catalyst, so that the extract obtained from the oligomerization step is optionally subjected to mild hydrogenation to hydrogenate the remaining carbon black bonds and reduce the formation of coke in the next step. Prehydrogenation Performed in the presence of a hydrogenation catalyst at 50 ° C to 400 ° C at a hydrogen pressure of 0.1 to 20 MPa and at a flow rate of: WHSV 0.1

L / h, preferably at 150-250 ° C, 1 to 10 MPa Hydrogen and 1 to 5 l / h. The prehydrogenation catalyst contains batchy group VIII and / or VIA metals. Preferably, the prehydrogenation hand catalyst is a Pd, Pt, Ni, iMo, or · Co • '1 Mo catalyst on a support which is aluminum and / or silica. ;; '' · '/ · i'

20055661 prh 02 -10-20199

Alternatively, deoxygenation may be carried out by Joko hydrodeoxygenation or by decarboxylation / decarbonylation. Hydrodeoxygenated (HDO) 1 / 5th deoxygenation rate is suitable for all feed materials. In the HD6 step, the oxygen as well as the oligomerized and optionally prehydrated stream 7 are passed through: a HDO catalyst bed comprising one or more catalyst beds. In the HDO step, the pressure is in the range of 0.1 to 20 MPa, preferably 1 to 15 MPa, highly edulfate

500 ° C, preferably 200-400 ° C, preferably at a temperature of 250-350 ° C and: 1 / flow rate - 10 1 / h, preferably WHSV 1-5 l / h, very preferably WHSV 1-3 1 / h. In the HDO step, specific dopants can be used which contain the elemental group Vili and / or VIA metal and / or aluminum and / or silica.

Preferably, the HD6 catalyst is a Pd, Pt, Ni, NiMo, or C0Mo catalyst supported on 7/7 aluminum and / or silica. / 7 7 i 7; 7 '7 7 7 7 / t:

If the feed contains carboxylic acids and / or carboxylation, the decarboxylation / decarbonylation reaction can be performed.

7 Decarboxylates in Io / Decarbonation Reaction Feed and Optional Diluent Joh / 2: · Particulate catalyst bed. : The reaction 107 takes place in the liquid phase and can: be carried out on a net basis. However, it is preferable to use a vapor stream according to the reaction temperature of the reaction mixture, depending on the feed temperature7, the pressure is 0-20 MPa preferably 0.1-5 MPa and the temperature is 200-400 ° C, preferably 250-350 ° C and the flow rate is WHSV. 0.1-10 l / h, 'eduIlisestifWHSV :: l · 7:: 5 1 / h. In the decarboxylation / decarbonylation step, 'specialty / 77 lytes containing elemental group VIII and / or VIA metals such as Pd, Pt,

Ni, NiMo-complete CoMo catalyst, such as aluminum and / or silica and / or activated carbon: Preferably, the decarboxylation / decarbonylation catalyst is Pd on carbon, · /: 7 in the Yun process when using a mixture of hydrogen and an inert gas such as nitrogen for the process. De to: v'DecarbOnylation step, the foreclosed / depleted functional groups and hydrogen and its carbon number were reduced by one carbon to remove the functional group. / 7 7 7/7/7

20055661 PRH 02 -10-20199 ;;;;; y <- If deoxygenation is carried out by decarboxylation / decarbonylation, then the oligomerization can be primed before the supply of the oligomerome step Contains saturated carboxylic acids and / or carboxylic acid esters. If the oligomerization is done after the decarboxylation / decarbonylation step, the feed of the ligation step contains decarboxylated / decarbonylated unsaturated compounds with a lower carbon number per feed: - y for the t .: .- / 1 - // ...- /: - .. ^ -.--. // -? Öy In the deoxygenation step of the invention, the HDO and decarboxylation / decarbonylation reactions described above may also occur at the same time so that yy: some · of the // functional groups to be treated will split carbon dioxide or carbon monoxide and some of the functional groups will be hydrogenated.

Optionally, after the deoxygenation step, the light fractions can be led to a separate isomerization step in which the hydrogen gas and hydrogenated component are introduced in an isome / y (w / w unit of 0.1-20 MPa, preferably / 5 to 10 / MPa / temperature) (1: 00- At a temperature of 500 ° C, preferably at 200 ° C, special catalysts containing a molecular sieve and 1 elemental group VIII metal, for example Pt and Pd, may be used in the isomerization step. The carrier may be 20 / aluminum and / or silica, yyy / / toy y yy. i · // il · \

After the oligomerization and deoxygenation steps of the components, the working stream can / may be optionally finalized to remove any double bonds and aromatics. If hydrogen is eliminated in the presence of a catalyst, this is called hydrogen finishing. In the hydrogen finishing step, the pressure is 1-20 MPa, preferably 5-15 MPa. The temperature is 50-500 ° C, preferably 200-400 ° C. In the hydrofinishing step, special catalysts containing metal / aluminum and / or silica may be used. Preferably, the hydrofinishing catalyst can also be carried out without hydrogen by removing the adsorbent of the polar components with thi

After the oligomerization, deoxygenation, and optional isomerization and finalization steps, the fraction is separated and separated into various types of fractions, for example, by distillation. Typical carbon number ranges for product components are: C1-C4 gas, C5-C10 gasoline, C1-C26 diesel, C18-C76 base oil. / <'; '' '2' ik '- //)) / // yj The resulting hydrocarbon or other hydrocarbon may be recycled to various process steps such as oligomerization or deoxygenation to increase conversion and selectivity. to control ',' '- / 1 /) ////' i T f '' ki? 4? In one embodiment of the invention, the ice oligomerized product may be further oligomerized by the addition of a process enzyme (stirring reaction reaction), or by recirculation of the already oligomerized product with the addition of a monomer. In this way it is possible to obtain 15 / extra-thick base oils having carbon numbers up to Cl 50 -C550 and which can / can be used to make thick lubricants and viscosity index enhancers. y t '/ s / // / / / / / / // // /// - / / i ktyUOTE / /' / - '/ y // - (- / k - / /) </. - / '/? k / k / - / o Surprisingly, it has been found that the process of the invention provides a high quality, non-volatile, hydrocarbon component of high biological origin having a biological origin with viscosity-ticmm irmTu j, i / s are excellent. The product is disrupted by carbon-carbon bonds.

As a by-product, a hydrocarbon / component suitable for use as a solvent, gasoline or diesel fuel or diesel fuel blast is obtained, preferably of biological origin. The diesel component or - C18-C24 base oil component can be iSo30 hydrogenated to improve cold performance. The β-blue component may be isomerized to increase the octane number. What if the process used / used post-oligomer 25

20055661 prh 02 -10-20199 '''''''' in the form of short-chain olefins or short-chain unsaturated carboxylic acids; · / To branch off the remaining double bonds, there is no need for isomerization. The carbon number index 5 ahxe of the base oil or base oil compound according to the invention depends on both the biological raw material used and the process of production. k The prior art base oil applications have a conventional carbon number range of Cl 8 to C76 and carbon grades of up to 50 C550. Aiming at a viscosity range of base oil of KV 100 of 4-7 rpm / s, the process according to the invention typically produces one carbon number of branched petroleum sulfur paraffin after feeds containing one carboxylic acid chain length after oligomerization and HDO step. k> k - <kkkk Also the carbon number range of k base oil · · or base oil component produced by the oligomerization and combined HDO and decarbokylation process according to the invention is' very narrow, typically with a C32 component, With C18kompo® monthly supply, the product has a carbon number range of C34-C36 with a target viscosity range k <KV 100 of 4-7 mm ² / s. When the feed · is a mixture of C16 and C18 components, the product's carbon number range is typically seven carbon wide. ' The carbon number of the base US120 of the invention can also be very high, even in the range of Cl50-C550k if desired _; Special oils are particularly suitable for viscosity enhancers and viscosity index enhancers. The carbonaceous and typical numbers of the bitter (I and 2) and prior art synthetic KV100 4-6 mm ² / s base oils (3-5) are shown in bold. The base oil or base oil component of the invention differs from the prior art products in terms of their molecular structure in terms of molar kk, as shown in the table.

30: In Table 2, naphthene structures are typical examples of a group of compounds. In the keniie examples, the C18 feed oligomeromer 1 had a carbon number of 26

20055661 prh 02 -10-20199 The range is C34-C36 and the oligomeric trimer 2 has a carbon number range of C51-C54, while those of known synthetic hydrocarbon base oils of the same viscosity class such as PAO have a C32-C48 or C30-C30 residual C10.

Table 2. Carbon numbers and typical structures of base oils

base oil Carbon number / FIMS-% Structure 1 C18syöttö Oligörneeridimeeri C34 / C35 / C36 acyclic <50% .. ..... ... ... ... .... .. ..... naphthenic; > 50% ...- ....-. - .... .... 2 C18 Input '' Oligomeeritrimeeri C51 / C52 / C53 / C54 3 PAOC16 C32 ·> about 60%; 7 / y j + C48 7 '' ····; about 40% y y y y y y 1 i 4 PAOCIO C30 about 80% y + C40 - - - 7 - n 20% 7 - / - 77 5 PIO y <7 C30-C48

20055661 prh 02 -10-20199

Saturated: Hydrocarbons are categorized by field ionization mass spectrometry (FlMS) according to their carbon and hydrogen non-conforming properties as follows · / 7 7

C (n) .H (2n / 2) yy / PARAFFINS yy y C (nj.H (2n) y mononaphtenes C (n) .H (2n-2) / / - / DINAFTEEN / C (n) .H (2n-4) / y / 7 TRINAPHENEES C (h) .H (2n-6) / / TETRANAFTEENIT C (n) .H (2n-8) '/ PEXTAN \ ETHENES

7 '777 7 7 7 7 1

757 ·· 7 ’7 7 / --2 / 7/7/7 7 7’ 4

7/7 7 7/7 // 5

7- / 7/7 / / - C y7 / 7? - / 7 ^: 7'Τ '·.'-'i.''.- ··

The percentages (FlMS%) in Table 2 refer to the groups of compounds determined by this method. ^^^^^^^^^^^^^^^^^^^^ 777/7/ 7-

7 Base Oil Corn Components of Table 2 are prepared as follows: 7/7 / / y /// y // / / 7 '// / 7/7 // y

1. The C18 / fatty acid dimer of tall oil, oligomerized and hydrogenated according to the invention? 7/7/1/7 / y 77 y y / 7; 2. The oil of the invention, prepared from tall oil, oleaginated and hydrogenated Cl 8

3. Made from 1-hexadecene by oligomerization with a heterogeneous catalyst

- PAO C16 / y /: / ''? / (// '(Ty / y yyl' / /: / - / 7 //// y / 'Ll'l /' y / - - / -.- / - / 77- / 77 - // / // ---: / --- / 1 /

PAÖ Cl 0 y prepared from 4.1-decene by homogeneous catalyst oligomerization Internal C15-C16 olefin> dimerimanal preparation: PIÖ / / 7 y / y

The oligomerized dimer and trimer components of the invention (structures 1 and 2 in Table 2) are branched by double bonds at the center of the C 18 hydrocarbon chain, wherein the tertiary-carbon-pairs in the molecule structure are of the C 1 -C 10 carbocyclic atoms. : a prepared dimer when the product of the invention is a Cl 6 and / or C 18 dimer. In addition, the product of the invention contains a significant amount of mononaphthenes, up to more than 50% FIMS. 7 y / 7 / y y y y? 7/7 / y

20055661 prh 02 -10-20199

In the process for the preparation of prior art polyalphaolefins, the reaction is carried out with boron trifluoride catalysts, in the presence of a double bond at the ends of the Cl0 chain, leaving one of the ethylene bonds between the tertiary carbons (Table 2, Strand 4). When the oligomerization is carried out in a heterogeneous manner, the twin bonds are displaced from the 'alpha position and at the same time the skeletal isomerization occurs, whereby:

7 1 to 10 methylene groups remain between the tertiary carbons (Table 2 'structure · 3, exemplified by 4 methylene groups). Similarly, when the oligomerization is carried out with a homogeneous catalyst, a hydrogenation step is obtained in the post-skeletal isomerization step, whereby the molecules of structure 4 of Table 2 additionally form double bonds near the C1-C3 side branches. The prior art PAO and PIO base oil components have predominantly alkyl moieties, but the product of the invention has, in addition to the alkyl moieties, naphthenic time moieties branched by ring structures.

1577/77 - 7 7i 777 i

The boiling point 77 of the high quality base oil obtained by the process of the invention · is at best below -40 ° C, so it is well suited for use in the cold conditions of demanding Vissa. The viscosity index of the product is even at its best

7 over 125, making it suitable for use in Group III Base Oil applications. <> 111777/7/7 777 1

7 7 Adding Various Short Chain Unsaturated Carboxylic Acids or Olefins to Biological Feeds · The molecular weight of the product can be adjusted to different applications> By cross-linking or oligomerizing with small fatty acid carboxylic acids or o>

form short branches in the main hydrocarbon chain of the fatty acid. When using a feed

For example, alpha-pinene, the product yields molecules in which the ring structure is in the side chain of the molecular chain. Edulfe is ol 7 7 · gomerized with one or two additional components. According to the invention, similar products tailored to the length of 30 liters of hydrocarbons can also be made from other

- 'carboxylic acids and other short-chain biocomponents. lighter,

20055661 prh 02-10-20199 branched and HDO treated components are suitable as well biodiesel pre-components. / R m 9 ^ 0 o

The organic base oil according to the invention comprises a product made from an organic raw material which according to the gas chromatographic assay t 'contains at least 90 wt%, preferably at least 95 wt% and particularly preferably at least 97 wt% saturated hydrocarbons. contains more than 40 FIMS% of mononaphtenes according to EIMS and allc * 3.0 FIMS% - preferably less than 1.0 FIMS% and very preferably less than 0.1 FlMS% of the mono-naphtha. up to 20 wt.% of novel paraffins, preferably up to 10 wt.%, particularly up to 5 wt.%, and most preferably up to 1 wt.

C £>

O *

: OO:

C \ l

T d

CD

C/O

O

O

CM k In the base oil or base oil component of the invention (the proportion of paraffinic (; carbon-free carbon atoms of all carbon atoms is> 60%, preferably> 70% and k particularly preferably> 75%), and the base oil or base oil component contains 10k%, preferably ( less than 5%, and particularly preferably%, as determined by the OINTT378 method. k k k k ^ k k k; k k k k k ((k k (y;. k k ((

The base oil or base oil component of the invention has a viscosity index of k (at least 1 (00, preferably at least 110, and particularly preferably at least 128; kk (- ((ASTM _: D ('227O)).'

A product according to the invention is branched in the carbon-carbon bond, which construction al (brings about an excellent low jähmepisteeh, not more than 0 ° C, preferably not more than IU 10 ° C, and particularly preferably not more than -35 ⁰ C 3 (((((((k · ό ) (? y

Mukaisenk invention viskosrt 4-7 mm ² / s basic oil or perusöl30 jykomponcntin liikuväl hi i li i is not more than 9 _carbons: preferably not more than 7 carbons, and c \ j

CM in

CM cd

xo

CM

CD o r

X tr

CD CD m m o o

CM very preferably · up to 3 carbon atoms (as determined by field ionisation spectra y / metric, FIMS). / ^ / / / v / / / o </ - // /

The base oil or base oil component of the invention has a sulfur content of less than

300 ppm, preferably less than 50 ppm and particularly preferably less than 1 ppm (ÄSTM D 'e 3120). 7 // '/ / ⁷ \ base oil or base oil component according to the invention, the nitrogen content is less than / 100 ppm, preferably less than? TO ppm and particularly preferably less than 1 ppm (ASTM D

4629). / / / / 7?

Volatility of the base oil or base oil component of the invention to the products; having a KV 100 of at least 4 mm ² / s is less than 20% by weight, preferably less than 15% by weight and particularly preferably less than <M 51581-2). 7 // // //;

'' 7-7. / ///// 77 / ry _Z

Bio-based products also contain carbon 14 isotopes due to their biological origin, which can be used as evidence of the use of renewable raw materials.

// // Typical ^! 4C content of a bio-based product is at least 100% as determined / • as a radioactive carbon concentration with ASTM D6866 as the starting point for atmospheric radio:

/ carbon content · in / 1950. When the product is used for processing other than // // 7 ^^^ ^l4 C-isotooppipitoisiius lower, however, -more than 90%, very preferably more than 99 / / /%. In this way, even a small amount of bio-based base oil can be identified from other hydrocarbon base oil Seas. / / / /: / /

25 /: / - / / // 7 / '-: /: /: // - /:

// Diesel Compound Adjustable by the Process of the Invention Applicable / / Product / Cetane Ratio / [epsilon] /; over / 55 / ϊ0 /; more than 60% by volume, preferably more than 99% by volume, and less than 30% by volume of aromatics, /

7 / bargain- ^c c ^c! i alle l td- 'ir-m; n okan. The product has a straight; %.

The diesel component has a cloud point below 0 ° C, preferably below / -15 ° C and particularly preferably below -30 ° C. Available diesel r - / / / / / /:: / / / / ϊ

/

20055661 PRH 02 -10-2019: The product is typically completely bio-based. The product according to the invention has carbon-carbon bonded side branches, which results in an extremely low cloud point. In addition, organic products contain ¹⁴ C isotopes due to their biological origin, which can be used as evidence of the use of renewable substances. The fully organic product has a ¹⁴ C content of at least 100%.

The flow of organic feed has a strong reduction in product composition and boiling range. In addition, distillation can be divided into carbon numbers, which can be tailored to different applications. Typical carbon numbers for dimeric products 10 with inputs having C16, C18, C20 tλ and C22 hydrocarbon chain lengths are C32, C36, C40 and C44 after hydrodeoxygenation and 2 C30, O after decarboxylation / decarbonylation.

C42. Since the product distillate moiety is primarily feed hydrocarbon dependent, narrow fractions are obtained. The base oil component of the narrow-boiling range obtained according to the invention has a very low volatility compared to similar products according to the prior art, <:; 't; ya y '

ADVANTAGES OF THE INVENTION

The process according to the invention and the product made with it have several advantages, among which may be mentioned e.g. the use of renewable raw materials to reduce greenhouse gas emissions of carbon dioxide instead of non-renewable raw materials. According to the invention, high quality ; For advanced peros oils, a bio-based raw material containing heteroatoms becomes a completely new type of raw material residue alongside conventional crude oil.

The raw materials for the process of the invention are globally adjustable, and the utilization of the process is not limited: initial investments, such as in the case of GTL technology. ό '' 'y y y';

G yy y ^ />

20055661 prh 02 -10-20199 '' '' '' 'The products of the process of the invention are for use and' disposal; · carbon3, which means that they do not increase the carbon dioxide content of the raw materials derived from these raw materials. p 2 y v p

Oligomerization under acidic conditions and subsequent deoxygenation yields a hydrolytically more stable base oil, which does not decompose under humid conditions, compared to esters or other base oils containing heteroatoms, including fatty alcohols. In addition, the saturated hydrocarbons have a higher degree of refraction resistance than the maleic fatty acids or fatty alcohol dimer-based base oils or ester base oils containing the corresponding unsaturated groups. The saturated hydrocarbon compound does not readily decompose as the esters which form corrosive acids.In the deoxygenation step, the alcohols, the esters or the carbonyl acids are removed and the mah; ? The heteroatoms of the impurity impurities obtained by the process of the invention are obtained in a nonpolar and saturated hydrocarbon complex. Upon oligomerization, the long-chain carboxylic acid derivatives form a structure in which the deoxygene '7 ha-ions after the ion are the side branches formed by the bridging chain. In Cl 2: 1 to C20: 1 oligomerization, the side branches are typically C3-CΠ

7 '· Hydrocarbon has an exceptionally low pour point for base oil applications, so it is liquid at very low temperatures and also has a good viscosity index. Made from saturated hydrocarbon sov ^^^? i dad without mixture restrictions and it is also compatible; With lubricant additives7 Isa. s' 7 7 '' 7 12 1); 7 7 ^

The base oil or base oil component according to the invention has a conventional oil; > very good technical properties compared to hydrocarbon base oils of the corresponding Viscosity class, especially when KV 100 is 4-7 mm ² / s. A narrow boiling range means that the product lacks a lightweight initial component, ie significantly lighter molecules than the average, which is reflected in a lower volatility of the product, which in practice leads to reduced emissions.

20055661 PRH 02-10-2019: The product also lacks molecules made up of heavier components, meaning 'heavier than average' molecules, which results in 'Excellent' cold properties. With the base oil or base oil component of the invention, the carbon and boiling range are determined by the mu 15-7 arc of the feed composition. The aim is to adjust the boiling range of prior art base oils by distillation of the product to the desired kinematic viscosity. The ointment has the advantage that the / base oil / carbonaceous region and the xylene boiling region are narrow, whereby the composition: contains the same size molecules that behave differently in the same OO ratio. : //.71/1/1 /: / - / 11 l y ... 7 /. 77. '. /

7 '17 7 7i07- 7 7 7 7 7 7' // p / V

With the parent oil component of the invention, the high viscosity index of the product indicates that the amount of viscosity index enhancer typically used in lubricant compositions can be reduced. It is generally known that, for example, engine oils have the VII most abundant component in engine oiling. In addition, reducing the amount of VII will result in significant cost savings. 7 <7 7 7 7- - -7 ^ - / :. - 7 7 7 1 1 7 77 77 /

The woxy base oil or base oil component of the process based on purified fatty acids based on natural fatty acids does not contain sulfur, nitrogen or extreme 20 'thiazide compounds such as traditional crude oil based products where it can be

-also used for ^: -in applications where / users are exposed to g oil or oil mist. In addition, the product of the invention has an Erinoffic / Response to antioxidants and antifouling agents already available in the art. lubricants made from perUlp can be extended and used 25/7 in colder conditions. 7/7 - 7 7 7 /// / 1 / / 1 / / / According to the invention, the base oil component is better than esters / 7 compatible with conventional crude oil based base oil components, Fis-cherTropsch process-based base oil components and carbohydrate base oils. . In addition, it has no similar problems with rubber 1 / esters with elastomers, such as, for example, sealing materials. / 11

20055661 prh 02 -10-20199 '''''' The advantages of the base oil or base oil component of the invention are also that it? 1 -Fill API API Stupid II, preferably Group III- Base Oil1 <1 and can be used in 'Engine Oil' compositions as other API '/ II Group II or III Class Base oils under the same exchange rules.''' PI p 'p'<? The invention; base oil or 'base oil based on renewable'-; resources, which is clearly evident from the ¹⁴ C isotope content of the product.

'p' The ¹⁴ C isotope content of the product is -100% for organic products and Ö% for crude oil products. The bio-based base '' - 'also determines at least 1% of starch content in the base oil at ¹⁴ C-isotope content. · 'P' p The process according to the invention - the 1-to-5 'medium isle which is suitable for use as a diesel component, also has' excellent cold characteristics and is therefore well suited for use in demanding cold conditions. m P '''' op P

An optional pre-hydrogenation step can reduce thiases such as dust merofem, ring formation and aromatization; which degrade the viscosityoffins of the products and cause the curing of the HDO catalyst 'P. '' P P p p ppp 01 - 0 p An optional recycling step for unreacted feeder components can be used to increase double bond reactions to increase product yield. o P p o

251'ό .ρ ·

In the invention, synthetic compounds of similar chemical structure may be used as a feed instead of or in addition to organic raw materials. t''p 'The invention will be illustrated by the following examples. However, it is to be understood that the invention is not intended to be limited to the embodiments described herein or

20055661 prh 02 -10-20199 to combinations thereof, and the invention may be carried out without departing from the claims set forth above, in particular as described "1," "1". '1 iilii iESIMERKlT // y; beat i 'i i liiiiii 11

Described in the following examples: The inventive ingredients have excellent properties, and the carbon number and distillation range ύ: very narrow. The process according to the invention has provided a molecular structure having good viscosity and cold properties.

The products are well suited for base oil components without a mixture limitation, and are compatible with other ingredients: ii: i ::; ^: i \ Example 1 ii ii -: ii ·: 1 ::: -: / '- i:: i' .il: / i / si i. '· / · ii iiHydrocarbon Component Preparation of Vegetable Oil liii 1 /' ii: 15i i 1 s '/ Lili / lilliii ..-.- 1-: 1 ii <il li 11:':

i i; A feed mixture containing 200 ml of soybean oil, 6 g of montmorillonite catalyst and 5 ml: 1 of distilled water was stained in a: Paff circular pressure reactor. 1 Temperature: raised to 270 ° C and the oil was allowed to oligomerize with slow stirring? for an hour. i i ii 1

Then, in the HDO step, the edo-oligomerized mixture was hydrogenated in a Parr1 high pressure reactor with a K i / NiMo / AboS catalyst to i-i-raffin. 200 ml of the oligomer germinated soybean mixture was hydrogenated at 325 ° C at i and 5 MPa hydrogen pressure until no acid groups were detected in the sample FT1R spectrum.

The reaction mixture was stirred at 300 rpm. The final product was distilled and 25 as the predominantly branched and cyclic C36 paraffin. -11 ii .1 i lii i: ''.

The characteristics of the hydrocarbon component obtained after the oligomerization and FIDO step are outlined in Table 3. Similarly, hydrocarbon compounds can be prepared from other double-bonded vegetable and fish oils and from 30 animal fats. i i i il li ii i: i: i: iilϋ

20055661 prh 02 -10-2019 λ Example 2 '/:

Hydrocarbons: manufacture of edible oil based carboxylic acids? I of methyl esters 7 /> '? :; 7-7; 7 7

7 The soybean oil was pretreated by basic esterification with methanol under basic conditions at 70 ° C and 0.1 TMP in the presence of sodium methoxide catalyst

7: Biphasic to form methyl esters of carboxylic acids. The reaction mixture was purified by acid and water washing and the carboxylic acid methyl ester M

Mocked. Soybean oil-based methyl ester-carboxylic acid has a following: 1016: 0 11%, 018: 0 20%, C18: 18 8%, 018: 25 54% and CT

The carboxylic acid methyl ester obtained above was oligonized in the Parr reactor pressure reactor. 200 ml of the feed and 6 g of the benzene catalyst were charged to the reactor, subjected to nitrogen purging twice to displace oxygen, then the temperature was raised to 350 ° C and the carboxylic acid methyl ester was allowed to oligomerize with slow stirring for 7.5 µM. 7 k 77 7 7 7 ^ 7

Then, in the HDO step, the dimeric methyl ester and trimer-4-methyl ester obtained above were hydrogenated separately as in Example 1, and the final product was distilled off, whereby and cyclic C54 paraffin. 7 ^ 7 7 7 7

7 The properties of the hydrocarbon component obtained after the pretreatment step (interesterification) and the oligomerization and HDO step are shown in Table 3. The product's ethereal properties are excellent and can also be prepared from other vegetable, animal and fish acid based carbohydrate-rich carbohydrates ^. methyl ester. Recycle unreacted monomers in increased yield. 77 7 77 7 77 7 7 7 7 77 77 37

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EXAMPLE 3: '''''''''''''''''' _? j 1

Preparation of the Hydrocarbon Component from Tall Oil-Based Carboxylic Acids · 'In the pretreatment step, tall carboxylic acids of tall oil were distilled. Then, · carboxylic acids were oligomerized in a Parr high pressure reactor or 200 g of feed mixture (carboxylic acids), 16 g of montmorillonite catalyst, and · 10 g of water were charged “1 / reactor”. The mixture was cooled and the catalyst was filtered off. From the reaction mixture, the monomer fraction was separated from the dimeric and trimeric acids on a silica column. 45% by weight of the carboxylic acid dimer was obtained. In the HDO step, the dimeric fraction obtained above was hydrogenated as in the example until the carboxylic acid peak had disappeared from the FTIR spectrum. Product from a branching / paraffin stock. The properties of the hydrocarbon component obtained after the oligomerization and HDO step are shown in Taste 3. Similarly, components can be prepared. also vegetable and fish oils containing animal fats based on free carboxylic acids other than tall oil or on double bonds released by hydrolysis

Example ^: E /: '111 j'. ' jl 1 ^Λ e 1 .1 '' ..1: 'Manufacture of hydrocarbon component from tall oil based 1 carbox

Using 1 '1' pre-hydration 1 il:: :::: 1: 1 / .1 11. ·. ·.

3511 'i': 'i': - / '113:': I- · 1 l i i

In the pre-treatment step, tall oil free: carboxylic acids were distilled. Feed mixture: no starch / predominantly C18 at 30 wt%, C18: 24 at 42 wt%, and 018: 319 wt% carboxylic fatty acids. In addition, the fraction contained 2%> resin blemishes. The tall oil carboxylic acids thus obtained were oligomerized in a Parr high pressure reactor. 200 g of the feed mixture, 16 µl of montmorillonite handwash and 10 g of water were charged to the reactor. To displace the oxygen, the nitrogen pressure was raised to 0.5 MPa and stirred for 600 rpm. Pressure

20055661 prh 02 -10-2019 'was drained off and the trituration was repeated. The temperature was then raised to 255 ° C and the carbocarbonyl warts were allowed to oligomerize with slow agitation for 2 hours. The mixture was cooled and the catalyst was filtered off. From the reaction mixture, the monomeric, dimeric and trimeric acids were separated on a silica column. Carboxylic acid dimer p

5 wt%. << '/ (/) Prior to the HDO step, the dimeric fraction obtained above was double-bonded in 450 mL of a Parr high pressure reactor with pre-sulfurized NiMo / AfiO 2 catalyst. r / min The dimeric acid was hydrogenated when no 7 twisted bonds were observed in the sample FTIR spectrum.s' ·· '' / • in cat 1 until ΕΉ had disappeared from the carboxylic acid ^

7 yeast; paraffin-containing, preterm-filtered milk, via L-End-product-derived / hardened, and cyclic C3 6 paraffin. / 7 y vk <

The properties of the oligomerization after the prehydrogenation and HDO step are shown in Table 3. The hydrocarbon component has excellent properties and very narrow molecular distribution. Similarly, hydrocarbons can be prepared from tall oil-based free / carboxylic acids or from hydrolysis-released double-bonded vegetable and fish oil or animal fat-based carboxylic acids. 7

Example 5 k / /?; 7 (? É; \ << ^Λ · 3 v / 'Preparation of hydrocarbon component from soybean oil-based carboxylic acid methyl esters and

The soybean oil was transesterified as in Example 2 with methanol to give the methyl esters of the carboxylic acids. The reaction mixture was purified by washing with acid and water. Finally, the carboxylic acid methyl ester was dried. Metyyliesteriri ^^^

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The 333 / - acid composition was as follows: C16: 011%, C18: 20%, Cl8: 18%, Cl8: 254% and 018: 366%. Above: The resulting soybean lime methyl ester was oligomerized in a Parr high pressure reactor with alpha-pinene in a molar ratio of 2: 1 using 8% benzene catalyst and 4% water. 200 ml of feed mixture was loaded into the reactor. For the displacement of the feed oxygen, the nitrogen pressure was raised to 0.5 MPa and the mixture was stirred at 600 rpm for a moment.

The pressure was released and the nitrogen was repeated. The temperature was then raised to 310 ° C, pressure 2 MPa and soybean oil methyl ester allowed to oligomerize with alpha-pinene

3 with slow stirring for 6 hours. '3 31: 3 3 3: 3/3 3; The oligomerized product was subjected to hydrodeoxygenation as in Example 1.

•: The monomers were distilled off from the final product to obtain: C28 pin branched: 3 N-isoparaffin; as well as a paraffinic di15-mer and trimer of carboxylic acid methyl ester in admixture. The properties of the resulting hydrocarbon component are shown in Table / 3. In a similar manner, branched hydrocarbon linkages can also be prepared from other double, double-bonded plant, animal and fish-based carboxylic acids or methyl carboxylic acid esters and suitable small molecules, preferably of biological origin. ';: 333/33 j :: 3333: 333 /// /: 33 /: 3

Example :: 3 // 3 /

Preparation of Heavy Hydrocarbon Compound from Acids 3 3: 3 3: 3: 3:33: ::

The tall oil was otherwise oligomerized as in Example 3, but the reaction was carried out slowly with stirring for 7 hours. The trimer fraction was separated from the reaction mixture by dimerizing and monomer fractions on a silica column. 3 /:: //: The trimer fraction obtained above was hydrogenated in the HDO step as in Example 1 after the 30th FTIR spectrum had lost the carboxylic acid peak. The product yielded branched cyclic paraffin. The product characteristics are shown in Table 33

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Similarly, hydrocarbon components can be prepared from free carboxylic acids based on non-soybean oil or from vegetable and fish oil or carboxylic fatty acids containing hydrolysis double bonds. 7 7 7 7 7 7: 7 /: / 7: / / 7/5 / 7- /:> / 7 // 7/7 / / - - /

Table 3. Properties of Processed Hydrocarbon Component / :: / /

Analysis E.g 1 E.g 2 7 E.g 3 77 / E.g M / / Out 5 // E.g 6 /; Method KV100 (minis) 5.2 6.0 5.6 6.6 5.4 25.1 ASTM D445 KV40 (mm7s) 28.9 35.8 32.0 38.0 31.8; 248.4 ASTMD445 νι, (-) 113 111 11-3- 129 104 129 ASTMD2270 Freezing point (° C) -9 -12 -57 -39 0 -9 ASTM D97 GC Distillation (° C) ASTMD2887 5% 394 398 380 335 50% 458 469 427 478 95% 482 626 495 647; GC-Noack, w-% 6.7 5.7 DIN 51581-2 Molecule] acacia, w-% 7: 7 ' aromatics 0.0 ASTM D2549 n-Paraffins <1 GC i-Parafhnit 28 FIMS mononaphtenes 57 FIMS dinaphthenes 15 FIMS Other naphthenes 0 FIMS Hiilityyppijakauina, % Of 7 -: - 7 DIN 51378 X (aromatics) 0 X (paraffins) 77.4 X (Naphthenes) 7 22.6 Sulfur, ppm 7 <1 ASTM D3120 / D4294 Nitrogen, ppm 1.5 ASTM D4629 ^l4 C,% -modem carbon 100

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Table 4. Properties of prior art base oils

Analysis API gpm HC-IDW API  GpIII HC-IDW API GpIII  sw API GpIH GTL API GpIV PAO Method KV100 (such as ^{the z} / p) 4.29 6.00 4.0 4.1 5.7 ASTMD445 KV40 (mrrr / s) 20.0 33.1 16.8 17.7 30 The STM D445 VI, p 122 128 140 139 135 ASTM D2270 Freezing point (° C) -18 -12 -21 -21 <-63 ASTMD97 GC Distillation (° C) ASTMD2887 5% 388 404 388 391 50% 421 459 421 430 95% 469 533 485 484 GC-Noack, w-% 13.3 5.8 DIN 51581-2 Molecular distribution p-% '< aromatics 0.0 0.0 0.0 0.0 0.0 ASTM D2549 paraffins 37.0 26.8 72.4 94.9 100 FIMS mononaphtenes 37.3 39.3 23.9 5.1 0.0 FIMS dinaphthenes 16.1 20.3 3.5 0.0 0.0 FIMS Other naphthenes 9.8 13.6 0.2 0.0 0.0: FIMS Carbon type pij aka u ma,% DIN 51378 X (aromatics) 0.0 0.0 X (paraffins) 67.1 76.4 XfNafteenit) 33.9 23.6 Sulfur, ppm <0.2 <0.2 <1 ASTM D3120 / D4294 Nitrogen, ppm <1 <1 <1 ASTM D4629 '* C% modem carbon 0 HC-IDW - hydrocracked, va base oil

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Example 7 ^: - 7 i; Demonstration of the bio-origin of the hydrocarbon component \;

The biobased hydrocarbon component of Example 6 was weighed into mineral base oil Group III base oil and mixed thoroughly. The first sample was weighed with a bio-based hydrocarbon dipohent of 0.5014; g and the Group II base oil component was added until the total mass was; 10.0 g; another sample weighed 1.0137 g of a bio-based hydrocarbon component and a Group II base oil cone

1 N was added until the total mass was 10.0232 g. Table 5 below summarizes the 10 measurement results. Radioactive carbon content is reported in "percent modern carbon", which is based on atmospheric radio carbon content in 1950.

? The radioactivity in the imaging ring is currently 107%. The value of the reference Dm indicates the method's background level. A value of 5 ^µC describes the ratio of stable carbon isotopes of ¹³ C / ¹²² C. This value can be used to coagulate the sample isotope fractionation. The last column indicates the actual result.

Table 5. Radiocarbon results. ; ό '<y y E; ; . ; <;

IWe i ¹⁴ C-Content,% 'IS ¹³ C'' Bio share,% 20; Mineral oil ' y 0, l ± 0.07 y -29.4 0 .3 y y Bio Oil y - y y i 106.7 ± 6.41 i-28.9 <l 3? ioo 33 3 '  'Mineral i + Bio 5 wt%? '5, OK 0.3 y' · j y 1-29.31 R 3 33 4.60 ± 0.28 3 yty Mineral i-rBio 10 wt% 10.8 ± 0. 3 i y  - 33-29.6 · 10.04 ± 0.29

σ> τΟ CM

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Claims (18)

Patent claim 7 · t /////////////////: /// 7: // 77 1 Base oil, characterized in that it consists of a mixture of hydrocarbons in 7 / which ·· 7: // 7 7 ': 7 // 7--: // 7 / / - hydrocarbon carbon numbers are between C18-C55O, and - 7 7 / / 7 // /: 7/7 / 7/7 7 at least 90% by weight of hydrocarbons are saturated, and 777/7 7 7: / 7 7 7. / 77 • 7- least 40% (FIM) of the hydrocarbons: mönonaftéWr _R is: and: 7 / + 7 - not more than 20% by weight of hydrocarbon hydrocarbons are straight-chain pear-raffles, 7 // - 7 below 10% by weight of the hydrocarbons is aromatic keel, and 7 7: //: / ::: / / k // --- below 3% (FIMS) of hydrocarbons is multipurpose. - the hydrocarbon carbon count intervals are not more than 9 carbon, and 7 .7 / 7 / ::: // · :: / • / · / - ¹⁴ C-iSotop content showing the biological / origin, of the entire amount of carbon is over 90% or ¹⁴ C -isotope level for 1950, and additionally Takes KVtOO, at least 4 mm ² / s and volatility 20 v% and the escape point: at most 0 ° C, which can be / produced so that an input comprising one or more components is seam: // selected ^? among the cooling numbers of C4-C38 carboxylic acids, esters of C4-C38 carboxylic acid tubes and C1-CT1 ato caffeic acid anhydrides and C4-C38 alcohols, and the feed contains mi ^^^^^^ and / or polyunsaturated compounds, are oligomerized in the presence of a cationic clay catalyst at a pressure of 0-10 MPa and at a temperature of 100-500 x and deoxygenated either as hydrodeoxygenation in the presence of hydrogen at a temperature of TOO - 500 ° C and a pressure of 0.1 - 20 MPa in the presence of a - hydrodeoxygenation catalyst or as a decarbonylation / decarboxylation /: / in the presence of a decarbonylation / decarboxylation catalyst at a / / temperature of 2ÖO-400 ° C and a pressure of 0-20 MPa. 7 n: / n- · · · 7 2. Basil oil according to pete hiccup 1, characterized in that the base liquor contains / 7 / at least 95% by weight of saturated hydrocarbons, at least 50 FIMS% by night ovens, at most 10:% by weight straight chain paraffins, below 5% by weight of aromatic carbon, its carbon count gap is highest and volatility below 15% by weight and at // the escape point at most -10 ° C 3. Base oil according to claim 1 or 2, characterized in that the base oil contains at least 97% by weight saturated hydrocarbons, at least 60 FIMS% monon nights, at most 5% by weight straight chain paraffins, below 1% by weight aromatic carbon, its carbon count 3 carbon and volatility density below 10% by weight and the escape point maximum -35 4. Base oil according to one of claims 1 to 3, characterized in that the ¹⁴ C-isotope content, which shows the biological origin of the base oil, of the total carbon content, is at least TOO% - \; i <i / ι <; I i ·· Process for the production of base oil according to any of claims 1 to 4, characterized in that the process comprises the stage where an input comprising one or more components is selected from among the carbon number C4-G38. 7 carboxylic acids, esters of: C4-C38 carboxylic acids and C1 -C11 alcohols, C4C38 carboxylic anhydrides and C4-C38 alcohols, and the feed contains at least 50% by weight of unsaturated and / or polyunsaturated compounds, oligomerized in the presence of a cationic clay catalyst at 0-10 MPa and at a temperature of 100-500 ° C and either deoxygenerate either hydrodeoxygenation in the presence of hydrogen at a temperature of 100-500 ° C and a pressure of 0.1-20 MPa in the presence of a hydrodeoxygenation catalyst or as decarbonylation / decarboxylation in the presence of a decarbonylation / decarboxylation catalyst at a temperature of 200-400 ° C and at a pressure of 0-20 Process according to claim 5, characterized in that the feed comprises one or more components selected from among the carbon numbers of C4-G24 carboxylic acids, esters of C12-C24 carboxylic acids and C1-C3 alcohols, 2C24 carboxylic anhydrides and C12-C24 alcohols <: / <? /// </ 7. _Process according to claim 5 or 6, characterized in that the feed comprises at least one raw material bioursprung, selected from triglycerides, fatty acids, esters of fatty acids and alcohols, and alkoholsyraanhydrider: fatty alcohols. <R ^^ / in. ? in σ> O CM ό CM o I tr CD CD ΙΌ LO CM Process according to patent claim 7, characterized in that; that the raw material of bio-origin is selected from a group consisting of R (e) plant fats, oils, waxes, animal fats, oils, waxes and fish fats, oils, waxes; ; b) carboxylic acids obtained by hydrolyzing, esterification or pyrolytic of plant fats, oils, ·· -wax, animal fats, oils, waxes; fish fats, oils, waxes, and mixtures of desSa, or free; c); esters · gériöm esterification of plant fats, oils, waxes, animal fats, oils, waxes, fish fats, oils, waxes and mixtures thereof; ; ; d) esters obtained by esterification of plant, animal and fish-based free; ; carboxylic acids with alcohols e) fatty alcohols obtained as reducing products of carboxylic acids as well; ; plant fats,>oils; - wax, animal fats ,; oils ,; -wax, fish fats, oils, -wax, and ;;;; mixtures thereof; ; --λ ;; '' I? ·;! ;; ; ; /; '^; 1 f) from recycled foodstuffs fats and oils, obtained by gene manipulation fats, waxes and oils, and '' </ i; v g) mixtures of the above, i; '' ';; ·; ; ;; in <; / Process according to any one of claims 5 to 8, characterized in that the feed contains at least · 80% by weight unsaturated and / or; polyunsaturated compounds; · ·; ; in; ';;;.;·;;;;;; ι1 '' · ^γ ; 10. Process; according to the patent claims as well; 5-9, characterized in that the oligomerization occurs at a temperature of 200-400 ° C. CM » CD O i CO CM X t £ 0th CO CD LO o CM Process according to any one of claims 5-10, characterized in that the oligomerization is carried out in the presence of a zeolite catalyst. ; Process according to any one of claims 5-11, characterized in that, when the feed contains carboxylic acids, no more than 10% by weight, advantageously 0-1% by weight of water is added to the feed at the oligomerization stage. /; ; ;;; ;; · ^; ; · Process according to any of Patrite claims 5-12, characterized in that: CM CM Process according to any one of claims 5-13, characterized in that the hydrodeoxygenation is carried out at a temperature of 200-400 ° C, with a pressure of 1-15 MPa with a flow velocity WHSV of 0.1-10 l / h. . <i CD CD LO LO Process according to any one of claims 5-14, characterized in that the hydrodeoxygenation catalyst is a Pd, Pt, Ni, NiMo or CoMokatalyzer with an aluminum and / or CM Process according to any one of claims 5-15, characterized in that the product at the oligomerization stage, prior to the hydrodeoxygenation, undergoes a prehydration in the presence of a hydrogenation catalyst at a temperature of 50 - 400 ° C with a hydrogen pressure of 0.1 - 20 MPa with a flow rate 1 · WHSV'pa 0.1 - 101 / h. < Process according to any one of claims 16, characterized in that the hydrogenation catalyst is a Pd, Pt, Ni, NiMo or CöMö catalyst with an aluminum and / or silica support. \ <. 18. A process according to any of claims 5-17, characterized in that the process feed or oligomerization product undergoes a decarbonylation / decarboxylation at a tern temperature of 250 - 350 ° C and with a pressure of 0.1 - 5 M P with a flow rate of hot WHSV. of 0.1 -10 1 / h. CM CD CO CM Process according to any one of claims 5-18, characterized in that the decarbonylation / decarboxylation catalyst is a Pd, Pt, Ni, NiMo 'or CoMo catalyst seats with' an aluminum and / or silica support and / or an active carbon carrier. . · I ·: c - c (£> (O CD CM Process 'according to any of claims 5-19, characterized in that after the oligomerization and deoxygenation phase' the product undergoes an isomerization in the presence of hydrogen gas at a pressure of 0.1-20 MPa, at a temperature of 100-500 ° C. in the presence of an isomerization catalyst. / ' 20055661 prh 02-10-2019 Process - according to: claim 20, characterized in that the isomensation catalyst contains a molecular sieve and a metal · from element group VIII with a Process according to any one of claims 5-21, characterized in that gasoline, solvent and diesel fractions are produced as a by-product.