Renewable paraffinic base oil

Abstract

A renewable paraffinic base oil comprises naphthenic compounds in an amount from 3 wt.% to 30 wt.% and paraffinic compounds in an amount of at least 50 wt.%. The naphthenic compounds comprise a mixture of 1 wt.% to 15 wt.%, mononaphthenic compounds and 1 wt.% to 12 wt.%, steranes, based on the weight of the renewable paraffinic base oil. At least 85 wt.% of the renewable paraffinic base oil has a boiling point greater than 280C. The renewable paraffinic base oil provides improved lubricity properties, and is suitable for use as a base oil in transformer fluids, battery thermal fluids, immersion cooling fluids, process oils and lubricating compositions.

Description

RENEWABLE PARAFFINIC BASE OILFIELD OF THE INVENTION

[0001] The present disclosure generally relates to a renewable hydrocarbon for use as a renewable paraffinic base oil. More specifically, the present disclosure relates to a renewable paraffinic base oil derived from hydroprocessing of renewable sources.BACKGROUND OF THE INVENTION

[0002] The demand for energy is increasing as a result of worldwide economic growth and development. This increase in the demand for energy has contributed to an increase in the amount of greenhouse gases and the overall carbon footprint. One area where demand is increasing is in the area of paraffinic base oils for applications such as transformer oils, battery thermal fluids and immersion cooling fluids and other process oil and lubricant applications. With decreasing reserves of crude petroleum oil that may be accessed and recovered easily, and increasing constraints on carbon footprints of such base oils, it may be desirable to develop routes to produce liquid base oils from renewable resources in an efficient manner. Renewable materials offers a source of renewable carbon. Examples of suitable renewable materials include vegetable oils, oils obtained from algae and animal fats, deconstructed materials such as pyrolyzed recyclable materials and wood, among others. Therefore, when using paraffinic base oils derived from renewable resources, it may be possible to achieve more sustainable CO2 emissions over petroleum-derived base oils. For renewable base oils to replace all or at least a portion of the carbon-based petroleum-based base oils, the renewable base oils should meet the required performance and emission specifications of the petroleum-derived base oils.

[0003] One technique for producing liquid transportation fuels from renewable resources is hydroprocessing. In order to maximise efficiency of manufacturing resources, it would also be desirable to use the same process to produce a paraffinic base oil that meets specifications required for base oil products, and that has desirable properties for use in lubricating and process oil compositions, as well as in insulating and transformer oils. Lubricity is an important characteristic of base oil products, as this is a measure of the capacity of a base oil for reducing friction.

[0004] Various patent applications have been published on renewable base oils. WO2018139971 relates to a light renewable base oil, for use as insulating oils and coolants with aVK40 of less than 4.5 mm2 / s, wherein the paraffinic mixture within the base oil consists mainly of C18 hydrocarbons. There appears to be no disclosure in WO2018139971 of C25 plus hydrocarbons or tetraplus naphthenics like steranes. US7888542B2 relates to a heavy base oil for use in lubricants. In the examples the VK40 of the base oils all exceed 28 mm2 / s. This base oil has a mononaphthenes content of at least 20 wt.% and a polynaphthenes content of less than 3 wt.%. No sterane content is specified. W020180782021A1 discloses a renewable insulating oil as heat transfer medium. The isoparaffins content exceeds 95 wt.% and the naphthenes content is less than 3 wt.%. No steranes content is stated, but it is believed to be well under 3 wt.%. EP-A-4321599 relates to a fluid with a high flash point and a pour point below - 65°C. This very low pour point is achieved by very high isomerization of the paraffins (specified as at least 99wt.% in the Examples). Although no steranes content is mentioned, it is believed to be negligible. Likewise, in W02021013860 the contents of light C17-C18 paraffins exceeds 90 wt.% and although the steranes content is not stated it is believed to be negligible.

[0005] WO18234188 and related US2020181527A1 (2020-06-11) describe a lubricating oil composition that includes a renewable base oil. This renewable base oil contains at least 60 wt.% C31 alkanes. Moreover, it is specified that the renewable base oil contains less than 2 wt.% of di-, tri-, tetra-naphthenes and higher. Although the steranes content of this base oil is not stated, in view of the low polynaphthenes it must be negligible.

[0006] Monnier et al. (US 5,705,722, 1998-01-06) relates to a process for producing liquid hydrocarbons boiling in the diesel fuel range from a feedstock comprising tall oil with a relatively high content of unsaturated compounds. The feedstock is hydroprocessed at a temperature of at least 350°C.

[0007] Germaine et al. (W02005 / 000999A1, 2005-01-06) discloses a process for preparing a base oil having a paraffin content of 75 - 95 wt.% by subjecting a mixture of a Fischer- Tropsch derived feed and a petroleum-derived feed to a catalytic pour point reducing treatment.SUMMARY OF THE INVENTION

[0008] According to the present invention there is provided a renewable paraffinic base oil comprising naphthenic compounds in an amount from 3 wt.% to 30 wt.% and paraffinic compounds in an amount of greater than 50 wt.%, wherein the naphthenic compounds comprise a mixture of mononaphthenic compounds and sterane compounds, wherein the amount of mononaphthenic compounds is in a range from 1 wt.% to 15 wt.%, based on the renewableparaffinic base oil, and wherein the amount of sterane compounds is in a range from 1 wt.% to 12 wt.%, based on the weight of the renewable paraffinic base oil, and wherein at least 85 wt.% of the renewable paraffinic base oil has a boiling point greater than 280°C.

[0009] Preferably, the renewable paraffinic base oil is produced from the hydroprocessing of a renewable resource comprising fats and oils. The renewable paraffinic base oil can be described as a HEFA (hydrotreated esters and fatty acids) product.

[0010] According to the present invention, there is further provided a process for producing the renewable paraffinic base oil herein comprising hydroprocessing a renewable feedstock comprising fats and oils, wherein the renewable feedstock resource comprises from 0.5 to 6 wt.% of unsaponifiables, by weight of the renewable feedstock.

[0011] According to the present invention, there is further provided a transformer oil composition comprising the renewable paraffinic base oil described herein.

[0012] According to the present invention, there is further provided a process oil composition comprising the renewable paraffinic base oil described herein.

[0013] According to the present invention, there is further provided a lubricant composition comprising the renewable paraffinic base oil described herein.

[0014] According to the present invention, there is further provided the use of the renewable paraffinic base oil described herein for improving lubricity. It has also been found that the renewable paraffinic base oil provides improved solubility, due to improved polarity.

[0015] The paraffinic base oils of the present invention have been found to have superior lubricity properties and are suitable for use in a wide range of applications, including transformer oils, battery thermal fluids, immersion cooling fluids, process oils, lubricant compositions, and the like.BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Embodiments of processes for producing the renewable base oil of the present invention will be better understood by referring to the following detailed description of preferred embodiments and the drawings referenced therein, in which:

[0017] Fig. 1 is one embodiment of a process for producing a renewable paraffinic base oil of the present invention, wherein a renewable feedstock is hydroprocessed;

[0018] Fig. 2 is another embodiment of a process for producing a renewable paraffinic base oil having a separate hydroisomerization zone;

[0019] Fig. 3 is a further embodiment of a process for producing a renewable paraffinic base oil, wherein a portion of the base oil is recycled to the hydroisomerization zone; and

[0020] Figs. 4 - 7 are still other embodiments of a process for producing a renewable paraffinic base oil, wherein a portion of the base oil is recycled to a hydrocracking zone and a hydroisomerization zone.DETAILED DESCRIPTION OF THE INVENTIONDEFINITIONS

[0021] The terms “linear paraffins” and “normal paraffins” or “n-paraffms” as used herein are intended to denote long straight chain saturated hydrocarbons such as, for example, normal hexadecane (n-C 16). The term “non-linear paraffins” as used herein is intended to denote saturated branched hydrocarbons such as, for example, mono-, di- and tri-branched paraffins (e.g. isohexadecane (iC 16)). The term “iso-paraffins” can be used interchangeably with the term ‘nonlinear paraffins’. Cycloparaffins, or naphthenes, are a class of hydrocarbons having a cyclic, nonaromatic structure. The terms “cycloparaffins” and “naphthenes” can be used interchangeably. Examples of naphthenes having one cycloparaffinic / naphthene ring include cyclohexane and cyclopentane.

[0022] The term ‘steranes’ as used herein means a class of cyclic compounds comprising at least four fused naphthenic rings. Preferably, at least one of the rings comprises 5 carbon atoms in the ring, and at least three of the rings comprise 6 carbon atoms in the ring. The steranes present in the renewable paraffinic base oil of the present invention are preferably derived from sterols that are part of the unsaponifiables present in the renewable feedstock. The sterols present in the renewable feedstock can be converted to steranes via the hydroprocessing process used for producing HEFA from fats and oils.

[0023] The term 'mononaphthenic compounds’ as used herein means naphthenic compounds having one naphthene ring. The term ‘dinaphthenic compounds’ as used herein means naphthenic compounds having two naphthene rings. The term ‘trinaphthenic compounds’ as used herein means naphthenic compounds having three naphthenic rings.

[0024] The term ‘unsaponifiables’ as used herein means the components of the renewable feedstock that fail to form soaps when treated with alkali and remain insoluble in water but solublein organic solvents. The amount of unsaponifiables present in the renewable feedstock can be measured according to standard test method ISO 3596.

[0025] The term ‘alkyl group’ as used herein in relation to dimers means straight chain or branched alkyl groups containing at least 8 carbon atoms. In a preferred embodiment, these alkyl groups are mostly branched chain alkyl groups. The total number of carbon atoms in all the side chain alkyl groups is at least 8.

[0026] The term “middle distillates” as used herein are hydrocarbons or oxygenated hydrocarbons recovered by distillation between an atmospheric-equivalent initial boiling point (IBP) and a final boiling point (FBP) measured according to standard ASTM distillation methods. ASTM D86 initial boiling point of middle distillates may vary from approximately 150°C to approximately 220°C. Final boiling point of middle distillates, according to ASTM D86 distillation, may vary from approximately 35O°C to approximately 380°C. “Naphtha” as used herein is one or more hydrocarbons or oxygenated hydrocarbons having four or more carbon atoms and having an atmospheric-equivalent final boiling point that is greater than approximately 90°C but less than approximately 200°C. A small amount of hydrocarbons produced in the process (approximately less than 5 wt.% of total C4+ hydrocarbons) boil at temperatures higher than those for the middle distillates as defined above. That is, these hydrocarbons have a boiling range similar to vacuum-gasoil produced by distillation of petroleum. Gasoline is predominantly naphtha-range hydrocarbons and is used in spark-ignition internal combustion engines. In the United States, ASTM D4814 standard establishes the requirements of gasoline for ground vehicles with sparkignition internal combustion engines. Gasoil (GO) / diesel is predominantly middle-distillate range hydrocarbons and is used in compression-ignition internal combustion engines. In the United States, ASTM D975 standard covers the requirements of several grades of diesel fuel suitable for various types of diesel engines. The HEFA product described herein is suitable for use as a renewable paraffinic base oil. The renewable paraffinic base oil comprises a mixture of mainly paraffinic compounds and a smaller amount of naphthenic compounds. The amount of naphthenic compounds is in a range from 3 wt.% to 30 wt.%, preferably in a range from 5 wt.% to 25 wt.%, more preferably in a range from 10 wt.% to 20 wt.%, by weight of the renewable paraffinic base oil. The level of paraffinic compounds is at least 50 wt.%, preferably greater than 50 wt.%, more preferably in a range of from 70 wt.% to 92 wt.%, even more preferably in a range from 76 wt.% to 90 wt.%, based on the renewable paraffinic base oil.

[0027] The naphthenic compounds comprise a mixture of mononaphthenic compounds and sterane compounds. The naphthenic compounds also preferably comprise dinaphthenic compounds, trinaphthenic compounds, and C32-C36 dimers. The amount of mononaphthenic compounds is in a range from 1 wt.% to 15 wt.%, more preferably in a range from 2 wt.% to 12 wt.%, more preferably in a range from 3 wt.% to 10 wt.%, by weight of the renewable paraffinic base oil. When present, the level of dinaphthenic compounds is in a range from 0.01 wt.% to 0.5 wt.%, more preferably from 0.05 wt.% to 0.3 wt.%, by weight of the renewable paraffinic base oil. When present, the level of trinaphthenic compounds is in a range from 0.02 wt.% to 1 wt.%, more preferably from 0.1 wt.% to 0.6 wt.%, by weight of the renewable paraffinic base oil. The level of sterane compounds in the renewable paraffinic base oil is in a range from 1 wt.% to 12 wt.%, preferably from 2 wt.% to 9 wt.%, by weight of the renewable paraffinic base oil. Preferably, the sterane compounds present in the renewable paraffinic base oil herein comprise up to seven naphthenic rings. Preferably, the steranes herein are C28 and C29 molecules. While not wishing to be bound by theory, it is believed that the sterane content contributes to the improved lubricity properties.

[0028] At least 85 wt.%, preferably at least 95 wt.%, of the renewable paraffinic base oil has a boiling point of at least 280°C according to ASTM method D2887. Preferably the renewable paraffinic base oil has an initial boiling point of at least 250°C. Preferably, the renewable paraffinic base oil has a final boiling point below 600°C.

[0029] Preferably, the renewable paraffinic base oil comprises less than 90 wt.% isoparaffins, more preferably in a range from 75 wt.% to 89 wt.% of isoparaffins, based on the renewable paraffinic base oil.

[0030] Preferably, the renewable paraffinic base oil comprises at least 50 wt.% of isoparaffins, preferably greater than 50 wt.% of isoparaffins, more preferably at least 70 wt.% of isoparaffins, even more preferably from 75 wt.% to 89 wt.% of isoparaffins, based on the weight of the renewable paraffinic base oil. Preferably, the renewable paraffinic base oil comprises at most 50 wt.% of n-paraffins, more preferably at most 20 wt.%, more preferably at most 10 wt.% of n-paraffins, by weight of the renewable paraffinic base oil.

[0031] Preferably, the renewable paraffinic base oil comprises from 1 wt.% to 12 wt.%, more preferably from 2 wt.% to 10 wt.%, of C32-C36 dimers, by weight of the renewable paraffinic base oil. The C32 to C36 dimers preferably comprise one or more naphthenic rings andtwo or more alkyl groups. The dimers are produced from olefins present in the renewable feedstock following the hydroprocessing treatment. The dimers preferably have more than 31 carbon atoms whilst the steranes preferably have less than 31 carbon atoms.

[0032] In a preferred embodiment, the heavy tail of the isomerized HEFA product from which the renewable paraffinic base oil is derived contains naphthenic compounds in the C28-C36 range, as a result of the presence of both the C32-C36 dimers and the C28-C29 steranes.

[0033] Preferably, the renewable paraffinic base oil has a C31 alkanes content of at most 60 wt.%, preferably <50 wt.%, <40 wt.%, <30 wt.%, <20 wt.%, <10 wt.%, <5 wt.%, based on the renewable paraffinic base oil.

[0034] Preferably, the renewable paraffinic base oil has a C17-C18 paraffins content of at most 90 wt.%, based on the renewable paraffinic base oil.

[0035] Preferably, the renewable paraffinic base oil has an aromatics content of at least 0.3 wt.%, more preferably from 0.3 to 6.0 wt.%, even more preferably from 0.3 to 3.0 wt.%.

[0036] Further, the renewable paraffinic base oil preferably has a kinematic viscosity at 40°C of at least 4.5 mm2 / s. The renewable paraffinic base oil preferably has a kinematic viscosity at 40°C of at most 12 mm2 / s.

[0037] Preferably, the renewable paraffinic base oil has a density at 15°C in a range from 750 to 850 kg / m3, more preferably from 770 to 830 kg / m3, even more preferably from 790 to 810 kg / m3, as measured according to ISO 12185.

[0038] Preferably, the renewable paraffinic base oil has a pour point in a range from -50 to -10°C, more preferably from -45 to -20°C, even more preferably from -42 to -32°C.

[0039] The renewable paraffinic base oil of the present invention is preferably prepared by the hydroprocessing of a renewable resource comprising fats and oils. Hydroprocessing biorenewable fats and oils (e.g., vegetable oil) generates hydrotreated esters and fatty acids (HEFA) that have low aromaticity (e.g., less than or equal to approximately 2 wt.%) and high linear paraffinic content (e.g., greater than or equal to approximately 90 wt.%) content. The high linear paraffinic content in the HEFA results in undesirable cold flow properties (e.g., cloud point and cold filter plugging point temperatures greater than 15°C). Therefore, HEFA derived base oil may not be suitable for use in climates in which the temperatures are less than 0°C. Accordingly, the HEFA derived base oil preferably undergoes additional processing to hydroisomerize the n- paraffins to generate iso-paraffins and improve the cold flow properties of the base oil.

[0040] As discussed in further detail below, the HEFA-derived distillate product may be generated from hydroprocessing renewable fats and oils. The HEFA-derived distillate product may be non-isomerized HEFA, isomerized HEFA or a combination of non-isomerized and isomerized HEFA.

[0041] In certain embodiments, the HEFA-derived distillate product may be highly n- paraffinic (e.g., having linear long chain hydrocarbon having 15 carbon atoms or more). As discussed above, the cloud point (CP) and cold flow pour point (CFPP) of certain n-paraffinic HEFA compositions, are undesirable due to the n-paraffinic content. Therefore, at least a portion of these n-paraffinic HEFA compositions generally undergo hydroisomerization to isomerize n- paraffins, thereby generating branched hydrocarbons (e.g., iso-paraffins) and decreasing the CP and CFPP temperatures. For example, the n-paraffinic HEFA composition may be hydroisomerized such that the amount of iso-paraffinic compounds in the HEFA composition results in a cloud point below approximately 0°C.

[0042] Embodiments of process units for carrying out the process of the present invention are described below and / or illustrated in the drawings. For ease of discussion, additional equipment and process steps that may be used in a process for producing fuel and / or chemicals from a renewable feedstock are not shown. The additional equipment and / or process steps may include, for example, without limitation, pre-treaters, heaters, chillers, air coolers, heat exchangers, mixing chambers, valves, pumps, compressors, condensers, quench streams, recycle streams, slip streams, purge streams, reflux streams, and the like.

[0043] Fig. 1 illustrates a general overview of one embodiment of the process of the present invention 10.

[0044] A renewable feedstock 12 is reacted in a hydroprocessing section 14 to produce a hydroprocessed effluent 16. Hydrogen may be combined with the renewable feedstock 12 stream before it is introduced the hydroprocessing section 14, co-fed with the renewable feedstock 12, or added to the hydroprocessing section 14 independently of the renewable feedstock 12. Hydrogen may be fresh and / or recycled from another unit in the process and / or produced in a HMU (not shown). In another embodiment, the hydrogen may be produced in-situ in the reactor or process, for example, without limitation, by water electrolysis. The water electrolysis process may be powered by renewable energy (such as solar photovoltaic, wind or hydroelectric power) togenerate green hydrogen, nuclear energy or by non-renewable power from other sources (grey hydrogen).

[0045] As used herein, the terms “renewable feedstock”, “renewable feed”, and “material from renewable sources” mean a feedstock from a renewable source. A renewable source may be animal, vegetable, microbial, and / or bio-derived or mineral-derived waste materials suitable for the production of fuels, fuel components and / or chemical feedstocks.

[0046] A preferred class of renewable materials are bio-renewable fats and oils comprising triglycerides, diglycerides, monoglycerides, free fatty acids, and / or fatty acid esters derived from bio-renewable fats and oils. Examples of fatty acid esters include, but are not limited to, fatty acid methyl esters and fatty acid ethyl esters. The bio-renewable fats and oils include both edible and non-edible fats and oils. Examples of bio-renewable fats and oils include, without limitation, algal oil, brown grease, canola oil, carinata oil, castor oil, coconut oil, colza oil, com oil, cottonseed oil, fish oil, hempseed oil, jatropha oil, lard, linseed oil, milk fats, mustard oil, olive oil, palm oil, peanut oil, rapeseed oil, pongamia oil, sewage sludge, soy oils, soybean oil, sunflower oil, tall oil, tall oil fatty acid (TOFA), tallow, used cooking oil, yellow grease, white grease, spent bleaching earth oil, and combinations thereof.

[0047] Another preferred class of renewable materials are liquids derived from biomass and waste liquefaction processes. Examples of such liquefaction processes include, but are not limited to, (hydro)pyrolysis, hydrothermal liquefaction, plastics liquefaction, and combinations thereof. Renewable materials derived from biomass and waste liquefaction processes may be used alone or in combination with bio-renewable fats and oils.

[0048] In the hydroprocessing section 14, renewable feedstock 12 is reacted under hydroprocessing conditions sufficient to cause a reaction selected from hydrogenation, hydrotreating (including, without limitation, hydrodeoxygenation, hydrodenitrogenation, hydrodesulphurization, and hydrodemetallization), hydrocracking, selective cracking, hydroisomerization, and combinations thereof. Preferably, the reaction is at least a hydrotreating reaction.

[0049] The reactions are preferably catalytic reactions, but may include non-catalytic reactions, such as thermal processing and the like. The hydroprocessing section 14 may be a single-stage or multi-stage. The hydroprocessing section 14 may be comprised of a single reactor or multiple reactors. In the case of catalytic reactions, the hydroprocessing section 14 may beoperated in a slurry, fluidized bed, and / or fixed bed operation. In the case of a fixed bed operation, each reactor may have a single catalyst bed or multiple catalyst beds. The hydroprocessing section 14 may be operated in a co-current flow, counter-current flow, or a combination thereof.

[0050] An example of a single-stage reaction is disclosed in van Heuzen et al. (US8,912,374, 16 Dec 2014), wherein hydrogen and a renewable feedstock are reacted with a hydrogenation catalyst under hydrodeoxygenation conditions. The whole effluent from the hydrodeoxygenation reaction is contacted with a catalyst under hydroisomerization conditions. The single-stage reaction may be carried out in a single reactor vessel or in two or more reactor vessels. The process may be carried out in a single catalyst bed, for example, using a multifunctional catalyst. Alternatively, the process may be carried out in a stacked bed configuration, where a first catalyst composition is stacked on top of a second catalyst composition.

[0051] The catalyst may be the same, a mixture or different throughout the hydroprocessing section 14. The hydroprocessing section 14 may comprise a single catalyst bed or multiple catalyst beds. The catalyst may be the same throughout the single catalyst bed, optionally there is a mixture of catalysts, or different catalysts may be provided in two or more layers in the catalyst bed. In an embodiment of multiple catalyst beds, the catalyst may be same or different for each catalyst bed.

[0052] The hydroprocessing catalysts may be used in bulk metal form, or the metals may be supported on a carrier. Suitable carriers include refractory oxides, molecular sieves, and combinations thereof. Examples of suitable refractory oxides include, without limitation, alumina, amorphous silica-alumina, titania, silica, and combinations thereof. Examples of suitable molecular sieves include, without limitation, zeolite Y, zeolite beta, ZSM-5, ZSM-12, ZSM-22, ZSM-23, ZSM-48, SAPO-11, SAPO-41, ferrierite, and combinations thereof.

[0053] The hydroprocessing catalyst may be any catalyst known in the art that is suitable for hydroprocessing. Catalyst metals are often in an oxide state when charged to a reactor and preferably activated by reducing or sulphiding the metal oxide. Preferably, the hydroprocessing catalyst comprises catalytically active metals of Group VIII and / or Group VIB, including, without limitation, Pd, Pt, Ni, Co, Mo, W, and combinations thereof. Hydroprocessing catalysts are generally more active in a sulphided form as compared to an oxide form of the catalyst. A sulphiding procedure is used to transform the catalyst from a calcined oxide state to an active sulphided state. Catalyst may be pre-sulphided or sulphided in situ. Because renewable feedstocksgenerally have a low sulphur content, a sulphiding agent is often added to the feed to maintain the catalyst in a sulphided form.

[0054] Preferably, the hydroprocessing catalyst is a hydrotreating catalyst comprising sulphided catalytically active metals. Examples of suitable catalytically active metals include, without limitation, sulphided nickel, sulphided cobalt, sulphided molybdenum, sulphided tungsten, sulphided CoMo, sulphided NiMo, sulphided MoW, sulphided NiW, and combinations thereof. A catalyst bed / zone may have a mixture of two types of catalysts and / or successive beds / zones, including stacked beds, and may have the same or different catalysts and / or catalyst mixtures. In case of such sulphided hydrotreating catalyst, a sulphur source will typically be supplied to the catalyst to keep the catalyst in sulphided form during the hydroprocessing step.

[0055] The hydrotreating catalyst may be sulphided in-situ or ex-situ. In-situ sulphiding may be achieved by supplying a sulphur source, usually H2S or an H2S precursor (i.e. a compound that easily decomposes into H2S such as, for example, dimethyl disulphide, di-tert-nonyl polysulphide or di-tert-butyl polysulphide) to the hydroprocessing catalyst during operation of the process. The sulphur source may be supplied with the feed, the hydrogen stream, or separately. An alternative suitable sulphur source is a sulphur-comprising hydrocarbon stream boiling in the diesel or kerosene boiling range that is co-fed with the feedstock. In addition, added sulphur compounds in feed facilitate the control of catalyst stability and may reduce hydrogen consumption.

[0056] When using a single-stage process as described in US8912374, any acidic zeolitic compound having hydroisomerizing activity may suitably be used. Such zeolitic compounds are known in the art. Examples of such zeolitic compounds include, but are not limited to, zeolite Y, zeolite beta, ZSM-5, ZSM-12, ZSM-22, ZSM-23, ZSM-48, SAPO-11, SAPO-41, and ferrierite.

[0057] From the viewpoint of maximizing the catalyst activity, the level of unsaponifiables in the renewable feedstock 12 used herein is preferably in a range from 0.4 to 6 wt.%, more preferably in a range from 0.5 to 4 wt.%, based on the weight of the renewable feedstock. In one embodiment of the present invention, especially from the viewpoint of maximizing the renewable paraffinic base oil yield, the level of unsaponifiables in the renewable feedstock 12 is preferably in a range from 2 wt.% to 6 wt.%, more preferably a 3 wt.% to 6 wt.%, even more preferably from 4 wt.% to 6 wt.%, based on the weight of the renewable feedstock 12. The unsaponifiables of the renewable feedstock 12 can be converted to steranes during hydroprocessing of the feedstock suchthat steranes are present at a certain level in the renewable paraffinic base oil. An advantage of the present invention is that lower grade feedstocks with higher amounts of unsaponifiable matter can be used to produce the renewable paraffinic base oil of the present invention. The resulting paraffinic base oil of the present invention has been found to have improved lubricity properties. While not wishing to be limited by theory, the improved lubricity properties are believed to be due to the high level of steranes present in the renewable paraffinic base oil of the present invention.

[0058] In a preferred embodiment, the renewable feedstock 12 has an iodine number of greater than 75 g iodine / lOO g of renewable feedstock 12, preferably greater than 90 g iodine / lOO g, more preferably greater than 100 g iodine / lOO g. The iodine number of the renewable feedstock 12 is related to the amount of olefins present in the feedstock 12. It is believed that at least a portion of the olefins present in the renewable feedstock 12 are converted to dimers following hydroprocessing of the renewable feedstock. The dimers are preferably C32-C36 dimers comprising one or more naphthenic rings, and two or more alkyl groups. The naphthenic rings present in the dimers are preferably C6 rings. The renewable paraffinic base oil of the present invention preferably comprises from 1 wt.% to 12 wt.%, preferably from 2 wt.% to 10 wt.%, more preferably from 3 wt.% to 8 wt.%, of C32-C36 dimers, by weight of the paraffinic base oil.

[0059] In certain embodiments, the renewable feedstock 12 may be pretreated prior to feeding to the hydroprocessing section 14 to remove impurities and other undesirable components.

[0060] Operating conditions in the hydroprocessing reactor include pressures in a range of from 1.0 MPaG to 20 MPaG, temperatures in a range of from 200 to 410°C and liquid hourly space velocities in a range of from 0.3 m3 / m3.h to 5 m3 / m3.h based on fresh feed. Preferably, the pressure is selected from a pressure in the range of 2.0 MPaG to 15 MPaG. Preferably, the temperature is in the range of from 200 to 400°C.

[0061] In certain embodiments, the total feed entering the hydroprocessing section 14 may have 50-20000 ppmw, preferably 700-8000 ppmw, most preferably 1000-5000 ppmw of sulfur, calculated as elemental sulfur. The term “total feed” is intended to denote the total of fresh feed, the optional sulphur additive and any optional diluting agent(s). The ratio of the hydrogen to the renewable feedstock 12 (excluding diluent) supplied to the hydroprocessing section 14 is in a range of from 200 to 10,000 normal L (at standard conditions of 0°C and 1 atm (0.101 MPa)) per kg of the renewable feedstock 12, preferably from approximately 500 to 8,000 NL / kg, more preferably from approximately 800 to 3,000 NL / kg.

[0062] Hydroprocessing of the renewable feedstock 12 in the hydroprocessing section 14 is an exothermic process. Therefore, to control any temperature increase in the catalyst bed(s), a staged supply of the renewable feedstock 12 and / or the hydrogen may be applied. In certain embodiments, the renewable feedstock 12 may be diluted, preferably by recycling a portion of a hydroprocessed effluent 16. Alternatively, a quench fluid (e.g., a hydroprocessed effluent 16 and / or recycle gas) may be fed to the hydroprocessing section 14 between each catalyst bed.

[0063] The hydroprocessing section 14 may be operated as a single-stage process or a multi-stage process. In one preferred embodiment, the hydroprocessing section 14 is operated as a single-stage process, in a co-current mode with one or more fixed beds. In one embodiment, the hydroprocessing section 14 has a single hydroprocessing reactor having one or more catalyst beds having the same multi-functional catalyst composition for catalysing at least one hydrotreating reaction, preferably hydrodeoxygenation, and a hydroisomerization reaction. In another embodiment, the hydroprocessing section 14 has a single hydroprocessing reactor with a first catalyst composition, having a hydrotreating function, stacked on top of a second catalyst composition, having an isomerization function. In another embodiment, the hydroprocessing section 14 has two or more hydroprocessing reactors, for at least two catalyst compositions. In yet another embodiment, the isomerization catalyst may also include a selective cracking function. Alternatively, a selective cracking catalyst may be provided in the same or different bed. Different numbers of catalyst beds may be used in each hydroprocessing reactor.

[0064] In another preferred embodiment, the hydroprocessing section 14 is operated as a multi-stage process, in a co-current mode with one or more fixed beds.

[0065] In one embodiment, the hydroprocessing section 14 has two hydroprocessing reactors. In another embodiment, the hydroprocessing section 14 has three hydroprocessing reactors, where the first and second reactors operate as a single-stage, and the third reactor operates in a multi-stage configuration with an intervening separation zone 20. Alternatively, the first and second reactors may operate in a multi-stage configuration with an intervening separation system, which may share some or all of the separator units of the separation zone 20 between the second and third reactors.

[0066] The hydroprocessed effluent 16 may then be directed to an optional separation zone 20 for separating the product of the hydrotreating reactions into a vapor phase effluent and a liquid hydroprocessed effluent 16.

[0067] The separation zone 20 has one or more separation units including, for example, without limitation, gas / liquid separators, including hot high- and low-pressure separators, intermediate high- and low-pressure separators, cold high- and low-pressure separators, high- and low-pressure strippers, integrated strippers, and combinations thereof. Integrated strippers include strippers that are integrated with hot high- and low-pressure separators, intermediate high- and low-pressure separators, cold high- and low-pressure separators. It will be understood by those skilled in the art that high-pressure separators operate at a pressure that is close to the hydroprocessing section 14 pressure, suitably 0 - 10 bar (0 - 1 MPa) below the reactor outlet pressure, while a low-pressure separator is operated at a pressure that is lower than a preceding reactor in the hydroprocessing section 14 pressure or a preceding high-pressure separator, suitably 0 - 15 barg (0 - 1.5 MPaG). Similarly, it will be understood by those skilled in the art that hot means that the hot-separator is operated at a temperature that is close to a preceding reactor in the hydroprocessing section 14 temperature, suitably sufficiently above water dew point (e.g., >10°C, preferably >20°C, above the water dew point) and sufficiently greater than salt deposition temperatures (e.g., >10°C, preferably >20°C, above the salt deposition temperature), while intermediate- and cold-separators are at a reduced temperature relative to the preceding reactor in the hydroprocessing section 14. For example, a cold-separator is suitably at a temperature that can be achieved via an air cooler. An intermediate temperature will be understood to mean any temperature between the temperature of a hot- or cold-separator.

[0068] In addition, the separation zone 20 may include one or more treating units including, for example, without limitation, a membrane separation unit, an amine scrubber, a pressure swing adsorption (PSA) unit, a caustic wash, and combinations thereof. The treating units are preferably selected to separate desired gas phase molecules. For example, an amine scrubber is used to selectively separate H2S and / or carbon oxides from H2 and / or hydrocarbons. As another example, a PSA unit may be used to purify a hydrogen stream for recycling to a stripper and / or a reactor in the hydroprocessing section 14.

[0069] A portion of the hydroprocessed effluent 16 from one or more separator units may be returned to a hydroprocessing section 14, for example, as a quench stream (not shown) or as a diluent (not shown) of feedstock 12. Recycle and quench streams may be made in a manner known to those skilled in the art. Preferably, the recycle stream is combined with the renewable feedstock. Alternatively, the recycle stream may be partitioned and added at two or more inlets to thehydroprocessing section 14. One or more quench streams are added in a manner known to those skilled in the art above catalyst beds in the hydroprocessing section 14.

[0070] The hydroprocessed effluent 16 is passed to a work-up section 30. The work-up section 30 includes one or more product recovery zones resulting in desired product streams. For example, the embodiment of Fig. 1 illustrates an off-gas stream 42, a naphtha boiling point range stream 44, a diesel boiling point range stream 48, and a renewable paraffinic base oil 52. In this embodiment, the off-gas stream 42 suitably comprises C1-C5 hydrocarbons, while the naphtha boiling point range 44 suitably comprises C4-C12 hydrocarbons in a boiling point range of from - 12°C to 204°C. The diesel boiling point range stream comprises C6-C26 hydrocarbons having a boiling point range of from 90°C to 400°C. In this embodiment, the renewable paraffinic base oil 52 has Cl 7+ hydrocarbons having a boiling point greater than 280°C.

[0071] In a preferred embodiment, the hydroprocessed effluent 16 (with or without a separation step) is passed to a hydroisomerization zone 34 under hydroisomerization conditions to cause a hydroisomerization reaction. The hydroisomerization reaction increases branching of the paraffinic compounds resulting from the hydrotreating zone 14, thereby improving the cold flow properties of a fuel.

[0072] As illustrated in Fig. 2, the separation zone 20 is optional. Where the hydroprocessed effluent is passed to the hydroisomerization zone 34 having a noble metal catalyst, the hydroprocessed effluent 16 is typically passed to the separation zone 20 prior to the hydroisomerization zone 34. Where the catalyst used for hydroisomerization has a noble metal, the separation zone 20 is provided to remove or at least substantially reduce components that poison or otherwise adversely impact the hydroisomerization catalyst. Where a non-noble metal is used for hydroisomerization, the separation zone 20 is optional.

[0073] The hydroisomerization catalyst may be any suitable catalyst composition known to those skilled in the art. Preferably, the hydroisomerization catalyst comprises a Group VIII metal. More preferably, the hydroisomerization catalyst further comprises a zeolitic material. The hydroisomerization catalyst may further comprise a binder and / or carrier, such as, without limitation, silica, alumina, silica-alumina, and combinations thereof. Preferably, the Group VIII metal is selected from the group consisting of platinum, palladium, nickel, and combinations thereof. When the Group VIII metal is Ni, the hydroisomerization preferably includes a Group VIB metal, preferably Mo or W.

[0074] The zeolitic material is preferably selected from the group consisting of Beta, COK- 7, EU-1, EU-2, EU-11, IZM-1, MCM-22, NU-10, ZSM-5, ZSM-12, ZSM-22, ZSM-23, ZSM-30, ZSM-35, ZSM-48, ZSM-50, ZSM-57, and combinations thereof.

[0075] The catalyst may be the same or different throughout the hydroisomerization zone 34. The hydroisomerization zone 34 may comprise a single catalyst bed or multiple catalyst beds. The catalyst may be the same throughout the single catalyst bed, optionally there is a mixture of catalysts, or different catalysts may be provided in two or more layers in the catalyst bed. In an embodiment of multiple catalyst beds, the catalyst may be same or different for each catalyst bed.

[0076] The hydroisomerization zone 34 is operated in the presence of hydrogen at a pressure in a range of from 1 MPaG to 30 MPaG and at a temperature in a range of from 260°C to 400°C. Preferably, the pressure is in a range of from 2 MPaG to 17 MPaG, and the temperature is in a range of from 300°C to 380°C. The LHSV is in a range of from 0.2 h-1 to 4 h-1 based on effluent 16. The ratio of the hydrogen gas to the liquid supplied to the hydroisomerization zone 34 is in a range of from 100 to 1500 normal L (at standard conditions of 0 °C and 1 atm (0.1 MPa)) per kg of the liquid.

[0077] Hydroisomerization is particularly advantageous for improving the production of kerosene for jet fuel. The product from the hydroisomerization zone 34 is directed to the work-up section 30. Various embodiments for the work-up section 30 may be considered. For example, without limitation, the work-up section 30 may be as described in WO2023 / 043792 or WO2023 / 043764 published 2023 March 23, incorporated by reference herein.

[0078] The work-up section 30 may be comprised of one or more unit operations. For example, the work-up section 30 may include separation units for separating a vapor effluent and a liquid hydroisomerization effluent (for example, of the type mentioned for separation zone 20), a product stripper for stripping entrained and / or dissolved gases from the hydroisomerizaton zone effluent, a naphtha stripper to produce the stripper offgas stream and a naphtha stream, a naphtha stabilizer column, a naphtha rectification column, a naphtha recovery column, an overhead separator, a vacuum fractionator, an atmospheric fractionator, and combinations thereof.

[0079] In the embodiment of Fig. 2, the work-up section 30 provides off-gas stream 42, naphtha boiling point range stream 44, a kerosene boiling point range stream 46, diesel boiling point range stream 48, and base oil 52. In this embodiment, the off-gas stream 42 suitably comprises C1-C5 hydrocarbons, while the naphtha boiling point range 44 suitably comprises C4-C12 hydrocarbons in a boiling point range of from -12°C to 204°C. The kerosene boiling point range stream 46 is preferably comprised of C6-C18 hydrocarbons having a boiling point range of from 90°C to 300°C. In one embodiment, the diesel boiling point range stream comprises C8-C26 hydrocarbons having a boiling point range of from 120°C to 400°C. In this embodiment, the base oil 52 has Cl 7+ hydrocarbons having a boiling point greater than 280°C.

[0080] In the embodiment of Fig. 3, a portion of the base oil 52, optionally also a portion of the diesel fraction 48, is recycled to the hydroisomerization zone 34. The work-up section 30 may include a further separation of the diesel boiling point range stream 48 into a light diesel stream that may be drawn off as a bleed stream, for example, while the heavy diesel stream is recycled with a portion of the base oil 52.

[0081] In the embodiments of Figs. 4 and 5, a portion of the base oil 52 and / or at least a portion of the diesel stream 48 is recycled to a hydrocracking zone 54 before contacting the hydroprocessed effluent 16.

[0082] The hydrocracking zone 54 operates under hydrocracking conditions sufficient to cause a hydrocracking reaction to produce a hydrocracked effluent.

[0083] The hydrocracking catalyst may be any suitable catalyst composition known to those skilled in the art. Preferably, the hydrocracking catalyst comprises a Group VIII metal. More preferably, the hydrocracking catalyst further comprises an acidic material.

[0084] The acidic material may be an amorphous acidic material, a crystalline acidic material, or a combination thereof. The amorphous acidic material may be, for example, without limitation, ASA. The crystalline acidic material may be selected from selected from the group consisting of Beta, COK-7, EU-1, EU-2, EU-11, IZM-1, MCM-22, NU-10, ZSM-5, ZSM-12, ZSM-22, ZSM-23, ZSM-30, ZSM-35, ZSM-48, ZSM-50, ZSM-57, and combinations thereof.

[0085] Preferably, the Group VIII metal is selected from the group consisting of platinum, palladium, nickel, and combinations thereof. When the Group VIII metal is Ni, the hydroisomerization catalyst preferably includes a Group VIB metal, preferably Mo or W.

[0086] The hydrocracking catalyst may further comprise a binder and / or carrier, such as, without limitation, silica, alumina, silica-alumina, and combinations thereof.

[0087] The hydrocracking zone 54 is operated in the presence of hydrogen at a pressure in a range of from 1 MPaG to 30 MPaG and at a temperature in a range of from 260°C to 400°C.Preferably, the pressure is in a range of from 2 MPaG to 18 MPaG, and the temperature is in a range of from 280°C to 400°C.

[0088] The hydrocracking conditions and catalyst are selected to favour cracking over branching.

[0089] In the embodiment of Fig. 4, the hydrocracking zone 54 is provided in a single- stage configuration above the hydroisomerization zone 34. In this embodiment, the portion of the base oil 52 and / or at least a portion of the diesel stream 48 is recycled to a single stage reactor comprising both the hydrocracking zone 54 and a hydroisomerization zone 34. The portion of the base oil 52 and / or at least a portion of the diesel stream 48 is first reacted in the hydrocracking zone 54. The hydrocracked effluent from the hydrocracking zone 54 is then passed to the hydroisomerization zone 34 where it is combined with the hydroprocessed effluent 16 for isomerizing the hydrocracked effluent and the hydroprocessed effluent 16 concurrently.

[0090] In the embodiment of Fig. 5, the hydrocracking zone 54 and the hydroisomerization zone 34 are provided in a two-stage configuration. In this embodiment, the portion of the base oil 52 and / or at least a portion of the diesel stream 48 is first reacted in the hydrocracking zone 54. The hydrocracked effluent from the hydrocracking zone 54 is then passed to the hydroisomerization zone 34 where it is combined with the hydroprocessed effluent 16 for isomerizing the hydrocracked effluent and the hydroprocessed effluent 16.

[0091] In the embodiments of Figs. 6 and 7, a portion of the base oil 52 and / or at least a portion of the diesel stream 48 is recycled to a hydrocracking zone 54 together with the hydroprocessed effluent 16.

[0092] In the embodiment of Fig. 6, the hydrocracking zone 54 is provided in a single- stage configuration above the hydroisomerization zone 34. In this embodiment, the portion of the base oil 52 and / or at least a portion of the diesel stream 48 is recycled to a single stage reactor comprising both the hydrocracking zone 54 and a hydroisomerization zone 34. The portion of the base oil 52 and / or at least a portion of the diesel stream 48 and the hydrotreated effluent 16 are first reacted in the hydrocracking zone 54. The hydrocracked effluent from the hydrocracking zone 54 is then passed to the hydroisomerization zone 34 for isomerizing the hydrocracked effluent.

[0093] In the embodiment of Fig. 7, the hydrocracking zone 54 and the hydroisomerization zone 34 are provided in a two-stage configuration. In this embodiment, the portion of the base oil 52 and / or at least a portion of the diesel stream 48 and the hydrotreated effluent 16 are first reactedin the hydrocracking zone 54. The hydrocracked effluent from the hydrocracking zone 54 is then passed to the hydroisomerization zone 34 for isomerizing the hydrocracked effluent.

[0094] In each of the process embodiments of Figs. 2 - 7, the hydroisomerization zone 34 optionally includes a hydrofinishing zone (not shown). During the hydroisomerization step and / or depending on the feedstock used (for example, cashew oil), some aromatics and / or trace olefins may be present in the effluent of the hydroisomerization zone. In this case, the hydrofinishing step is preferably provided to reduce the aromatic content of the product stream(s).

[0095] The hydrofinishing components may be used in bulk metal form, or the metals may be supported on a carrier. Active metals for hydrogenation include catalytically active metals of Group VIII and / or Group VIB, including, without limitation, Ni, Co, Mo, W, and combinations thereof. Preferably, the Group VIII metal is selected from the group consisting of platinum, palladium, nickel, and combinations thereof. Suitable carriers include refractory oxides. Examples of suitable refractory oxides include, without limitation, alumina, ASA, titania, silica, and combinations thereof.

[0096] The renewable paraffinic base oil can be used in a range of transformer oils, battery thermal fluids, immersion cooling fluids, lubricant and process oil compositions in an amount of from at least 5 wt.% to 100 wt.%, by weight of the total composition.EXAMPLES

[0097] The following non-limiting examples of embodiments of the process of the present invention as claimed herein are provided for illustrative purposes only.Example 1 (Preparation of HEFA base oil)

[0098] In a reactor, two catalyst beds were placed in a stacked bed configuration: a bed of 31.25 mL of a hydrodemetallization and hydrogenation catalyst comprising 2 wt.% Ni and 8 wt.% Mo on a support of alumina, was placed above a bed of 93.75 mL of a hydrodeoxygenation catalyst comprising 4 wt.% Ni and 15 wt.% Mo on alumina. The catalyst in the hydrodemetallization and hydrogenation catalyst bed was 1 :2 diluted with 0.1 mm diameter silicon carbide particles, while the hydrodeoxygenation catalyst bed was 1 : 1.5 diluted with 0.2 mm silicon carbide particles. The silicon carbide particles were applied to mitigate reactor wall effects that could disturb the uniform liquid distribution over the catalyst bed cross section. The temperature of both catalyst beds was controlled by means of an oven. The temperature of both catalyst beds was set at 310°C.

[0099] A feedstock consisting of distillers corn oil with an iodine value of 124 g 12 / 100g (ISO 3962) and 2.15 wt.% unsaponifiable matter (ISO 3596) was supplied to the catalyst bed at a WHSV of 1 g fresh oil per mL catalyst per hour. The feedstock was spiked with 0.34 wt.% SULFRZOL® available from Lubrizol as a hydrogen sulphide precursor to keep the catalyst sulphided as the sulphur concentration in the distillers corn oil was 16.7 ppmw. The reactor was operated with recycling a liquid fraction of the hydrocarbon effluent at a volumetric ratio of 1.8 to 1 compared to the fresh feed. A gas stream comprising 100 vol% hydrogen was supplied at a gas- to-oil ratio of 875 NL / kg on the basis of the fresh feedstock. The total pressure at the reactor outlet was 75 bar (gauge).

[0100] The degree of conversion of the distillers corn oil feedstock was determined in multiple ways. The hydrocarbon liquid was analysed using pyrolysis and two dimensional gas chromatography to determine the concentration of organic oxygen and molecular composition. The gaseous effluent was analysed using gas chromatography.

[0101] The conversion of organic oxygen was larger than 99% with a concentration of 200 ppmw elemental oxygen in the effluent. The hydrocarbon liquid consisted of more than 94 wt.% of paraffins, while the concentration of steranes and dimers, was 1.17 wt.% and 1.92 wt.%, respectively. This hydrocarbon liquid was subsequently used as the feedstock for the rest of the process.

[0102] A catalyst bed consisting of 30 mL of a hydroisomerisation catalyst comprising 0.7 wt.% Pt on a carrier comprising 75 wt.% silica and 25 wt.% zeolite ZSM-12 was placed in a reactor. The catalyst was 1 : 1 diluted with 0.05 mm diameter silicon carbide particles. The silicon carbide particles were applied to mitigate reactor wall effects which could disturb the uniform liquid distribution over the catalyst bed cross section. The temperature of the bed was controlled by means of an oven. The catalyst bed was operated at 340°C. The hydrotreated effluent produced above was supplied to the catalyst bed at a WHSV of 1.0 g fresh liquid per mL catalyst per hour. A gas stream comprising 100% vol% hydrogen was supplied to the top bed at a gas-to-oil ratio of 500 NL / kg. The total pressure at the reactor outlet was 73 barg (7.3 MPag).

[0103] The degree of conversion of the feedstock was determined in multiple ways. The hydrocarbon liquid was analyzed using ASTM D2887 simulated distillation to determine the boiling range distribution. The cloud point and density were measured using the ASTM D2500 and ASTM D4052 methods.

[0104] The gaseous effluent was analyzed using gas chromatography.

[0105] The collected hydrocarbon liquid effluent was distilled offline into a light product fraction and a heavy fraction referred to as a base oil product fraction. The renewable paraffinic base oil product fraction was characterized using two dimensional gas chromatography and ASTM D2887 simulated distillation to determine the molecular composition and the boiling range.

[0106] The base oil had an ASTM D2887 initial boiling point of 282.5°C and its composition is presented in Table 1.

[0107] The compositional details of the renewable paraffinic base oil produced in Example 1 are set out in Table 1 below.Table 1

[0108] Physical and chemical properties of the renewable paraffinic base oil produced in Example 1 are set out in Table 2 below. By way of comparison, Table 2 also sets out the properties of GTL-based isoparaffinic process oils, X409 and X411, commercially available from Shell (Comparative Examples A and B, respectively).Table 2*est. = estimated / normalised based on virtually 0 wt.% aromatics

[0109] This data shows that the HEFA base oil of Example 1 has a very paraffinic structure (containing 78 wt.% of iso and normal paraffins) and contains virtually no sulphur, similar to GTL- based products. Hence it is very suitable for the following lubricant applications, either as a blend component or even up to 100% in some lubricants: crop protection spray oils, defoamers, fertilizers, adhesives, optical cable oils, petroleum jelly, leather auxiliaries, thermoplastic elastomers, vaccination fluids, agriculture oils, fertilizers oils, plant protection fluids, dust suppressants, extender fluids, carrier oils for additive concentrates, textile aids, polishes, impregnation of coke, plasticizer for elastomers, thermoplastic elastomers and silicons, print inks, shoe molded parts, road-marking, metalworking fluid, cutting and grinding oils, quenching oil, form oil / mould release oil, deform work oil (concrete mould oil), refrigerator oils, heat transfer oils, transformer oils, shock absorber fluids, calibration fluids, bearing and circulation oils, hydraulic oils, turbine oils, dielectric immersion cooling fluids, battery thermal fluids for stationary and mobile applications, power steering fluids, greases, pneumatic tool lubricants, engine oils, marine oils, gas engine oils, compressor oils, cosmetic oils, oils for consumer care.Example 2

[0110] Two transformer oil compositions were formulated (Example 2 and Comparative Example C). The transformer oil composition of Example 2 contained 99.7 mass % of therenewable paraffinic base oil of Example 1 and 0.3 mass % Butylated Hydroxy Toluene (BHT) antioxidant additive. Comparative Example C contained 99.7 mass % of GTL 3 base oil (a GTL- based oil commercially available from Shell having a kinematic viscosity at 100°C of approximately 3 mm2 / s) and 0.3 mass % of Butylated Hydroxy Toluene (BHT) antioxidant additive. The transformer oil compositions were subjected to oxidation tests which are key tests to predict the lifetime and stability of the compositions. The results of these experiments are set out in Table 3 below.Table 3

[0111] The features of the renewable paraffinic base oil produced in Example 1 allow it to be useful as a blending component for transformer fluids according to IEC 60296 and ATSM D 3487, the most common industry specs for transformer liquids based on hydrocarbons. The results in Table 3 demonstrate that the renewable paraffinic base oil of Example 1 can be used successfully in a transformer fluid formulation. Example 2 has been shown to meet the ASTM D 3487 and theTEC 60296 (Type A, high grade) specifications. In particular, Example 2 provides comparable results in sludge and total acid number as Comparative Example C. This is a good result as GTL is known to have excellent oxidation stability.Lubricity Measurements

[0112] The lubricity of the HEFA paraffinic base oil from Example 1 was compared with that of a blend of GTL solvents of comparable kinematic viscosity (Comparative Example D). The lubricity was determined using an HFRR test method (according to ISO12156). No lubricity improvers were added to the base oils. The results are set out in Table 4 below.Table 4

[0113] Inspection of Table 4 reveals that although the GTL based sample has a slightly higher viscosity than the renewable sample, both the wear scar diameter and the average friction coefficient of the renewable base oil of Example 1 are surprisingly lower and hence better than those of the GTL derived sample. These results are surprising as normally the higher the viscosity, the lower (better) the wear scar.

Claims

CLAIMS1. A renewable paraffinic base oil comprising naphthenic compounds in an amount from 3 wt.% to 30 wt.% and paraffinic compounds in an amount of greater than 50 wt.%, wherein the naphthenic compounds comprise a mixture of mononaphthenic compounds and steranes, wherein the amount of mononaphthenic compounds is in a range from 1 wt.% to 15 wt.%, based on the weight of the renewable paraffinic base oil, and wherein the amount of sterane compounds is in a range from 1 wt.% to 12 wt.%, based on the weight of the renewable paraffinic base oil, and wherein at least 85 wt.% of the renewable paraffinic base oil has a boiling point greater than 280°C.

2. The renewable paraffinic base oil according to Claim 1, wherein the amount of sterane compounds is in a range from 2 wt.% to 9 wt.%, based on the renewable paraffinic base oil.

3. The renewable paraffinic base oil according to Claim 1 or 2, wherein the renewable paraffinic base oil has a kinematic viscosity at 40°C of greater than 4.5 mm2 / s.

4. The renewable paraffinic base oil according to any of Claims 1 to 3, wherein the renewable paraffinic base oil has a kinematic viscosity at 40°C of less than 12 mm2 / s.

5. The renewable paraffinic base oil according to any of Claims 1 to 4, wherein the renewable paraffinic base oil has a C31 alkanes content of less than 60 wt.%, based on the renewable paraffinic base oil.

6. The renewable paraffinic base oil according to any of Claims 1 to 5, wherein the renewable paraffinic base oil has a C17-C18 content of less than 90 wt.%, based on the renewable paraffinic base oil.

7. The renewable paraffinic base oil according to any of Claims 1 to 6, wherein the renewable paraffinic base oil has an initial boiling point of greater than 250°C.

8. The renewable paraffinic base oil according to any of Claims 1 to 7, wherein the renewable paraffinic base oil has a final boiling point below 600°C.

9. The renewable paraffinic base oil according to any of Claims 1 to 8, wherein at least 95 wt.% of the renewable paraffinic base oil has a boiling point greater than 280°C.

10. The renewable paraffinic base oil according to any of Claims 1 to 9, wherein the renewable paraffinic base oil is a hydroprocessed ester of fatty acid generated from hydroprocessing a renewable resource comprising fats and oils.

11. The renewable paraffinic base oil according to any of Claims 1 to 10, wherein the renewable paraffinic base oil comprises greater than 50 wt.%, preferably greater than 70 wt.% of iso-paraffinic hydrocarbons.

12. The renewable paraffinic base oil according to any of Claims 1 to 12, wherein the renewable paraffinic base oil comprises less than 50 wt.%, preferably less than 20 wt.%, more preferably less than 10 wt.% of n-paraffinic hydrocarbons.

13. The renewable paraffinic base oil according to any of Claims 1 to 12, wherein the naphthenic compounds further comprise from 1 wt.% to 12 wt.% of C32-C36 dimers, by weight of the paraffinic base oil.

14. The renewable paraffinic base oil according to Claim 13 wherein the C32 to C36 dimers comprises one or more naphthenic rings and two or more alkyl groups.

15. The renewable paraffinic base oil according to according to any of Claims 1 to 14, wherein the renewable paraffinic base has an aromatics content of greater than 0.3 wt.% as measured by ASTM D2140.

16. A process for producing a renewable paraffinic base oil according to any of Claims 1 to 15 comprising: hydroprocessing a renewable feedstock comprising fats and oils, wherein the renewable feedstock comprises from 0.4 to 6 wt.% of unsaponifiables (measured according to ISO 3596).

17. The process according to Claim 16, wherein the renewable feedstock has an iodine number of greater than 75g iodine / lOOg of renewable feedstock.

18. A transformer oil composition comprising the renewable paraffinic base oil according to any of Claims 1 to 15 or the renewable paraffinic base oil produced according to the process of Claim 16 or 17.

19. A process oil composition comprising the renewable paraffinic base oil according to any of Claims 1 to 15 or the renewable paraffinic base oil produced according to the process of Claim 16 or 17.

20. A lubricant composition comprising the renewable paraffinic base oil according to any of Claims 1 to 15 or the renewable paraffinic base oil produced according to the process of Claim 16 or 17.

21. A battery thermal fluid or immersion cooling fluid comprising the renewable paraffinic base oil according to any of Claims 1 to 15 or the renewable paraffinic base oil produced according to the process of Claim 16 or 17.

22. Use of a renewable paraffinic base oil according to any of Claims 1 to 15 or the renewable paraffinic base oil produced according to the process of Claim 16 or 17, for improving lubricity.

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