Electrotechnical fluid and method for its manufacture

Abstract

A method for producing an electrotechnical fluid composition is described, comprising the steps of subjecting a renewable feedstock comprising free fatty acids and glycerides to ketonization under ketonization conditions, subjecting the ketonized renewable feedstock to hydrotreatment under hydrotreatment conditions to obtain a renewable paraffinic intermediate product, and subjecting the renewable paraffinic intermediate product to at least one fractional distillation to obtain an electrotechnical fluid composition, the electrotechnical fluid composition meeting the requirements according to the IEC 60296 (2012) international standard.

Description

[Technical Field]

[0001] The present invention relates to a method for producing an electrotechnical fluid composition obtained from renewable raw materials, to the composition produced using said method, and to the use of said composition. [Background technology]

[0002] Electrotechnical fluids, either liquid or gaseous, are used in electrical equipment such as transformers, capacitors, switchgear, bushings, etc. Electrotechnical fluids typically function as an electrical insulating medium separating high voltage and earthed parts of the equipment, and as a cooling medium to transfer heat generated within the equipment. In addition to the above basic functions, electrotechnical fluids must meet other necessary and desirable requirements, such as a long operating life, operation over a wide temperature range, suitable kinematic viscosity, and minimal environmental impact.

[0003] In the field of electrotechnical fluids, there is a growing need to target sustainable, bio-based, and recycled alternatives. Although the demand for products prepared from renewable feedstocks is increasing, the use of renewable raw materials for the production of electrotechnical fluids that also meet the standard requirements for such fluids has been difficult, making the use of renewable raw materials for this purpose problematic.

[0004] US Patent No. 5,929,999 (by Neste Oil Oyj) describes a composite feed that is diluted with hydrocarbons and processed by pre-hydrogenation, ketonization, hydrodeoxygenation, stripping, hydroisomerization, optional hydrofinishing, and distillation to renewable base oil, renewable diesel, and renewable gasoline.

[0005] Patent Document 2 discloses a renewable hydrocarbon-based insulating fluid containing more than 70% isoparaffin. The disclosure does not teach a method for producing a fluid that meets the required performance, or a composition of a fluid that meets the required performance.

[0006] Patent Document 3 discloses an electrotechnical fluid for electric vehicles having a boiling point in the range of 200°C to 400°C and a boiling point range below 80°C, containing more than 95% by weight of isoparaffins and less than 3% by weight of naphthenes, having a biocarbon content of at least 95% by weight, and containing less than 100 ppm by weight of aromatics. The disclosure does not teach a method for producing a fluid that meets the specification requirements or a composition of a fluid that meets the specification requirements. [Prior art documents] [Patent documents]

[0007] [Patent Document 1] International Publication No. 2007 / 006879 [Patent Document 2] International Publication No. 2014 / 128227 [Patent Document 3] International Publication No. 2018 / 078024 Summary of the Invention

[0008] The object of the present invention is to provide a method for producing a hydrocarbon composition suitable for use as an electrotechnical fluid composition, which alleviates the above-mentioned drawbacks. The present invention also relates to an electrotechnical fluid composition that meets the requirements according to IEC 60296, and the electrotechnical fluid composition that can be prepared by said method. Furthermore, the present invention relates to the use of the electrotechnical fluid composition.

[0009] The inventors have surprisingly found that a side stream of a renewable base oil (RBO) process can be used for the production of electrotechnical fluids that meet the standard requirements for such products according to IEC 60296. The inventors have surprisingly found that a portion of the side stream from the RBO process can be used to produce an electrotechnical fluid composition that meets the standard requirements, thereby reducing waste streams and resulting in full valorization of the renewable raw materials, i.e., the feedstocks used in the RBO process. This results in a more environmentally friendly process, as waste streams from the RBO process are reduced and instead used as raw materials for the electrotechnical fluid composition, and the amount of other types of raw materials that would otherwise be used in the production of the electrotechnical fluid composition is also reduced.

[0010] In a preferred embodiment, the electrotechnical fluid composition is used as a transformer oil and has the advantage of less evaporation than known transformer oils.

[0011] One or more example embodiments are set forth in more detail in the description that follows. Other features will be apparent from the description and from the claims. [Brief explanation of the drawings]

[0012] [Figure 1] FIG. 1 is a diagram illustrating a process of one embodiment of the present invention. DETAILED DESCRIPTION OF THE INVENTION

[0013] The following embodiments are illustrative. Although the specification may refer to "an," "one," or "some" in several places, this does not necessarily mean that each such reference is to the same embodiment or that the feature applies only to a single embodiment. Single features of various embodiments may be combined to provide other embodiments. Furthermore, the words "comprising," "containing," and "including" should not be understood to limit the described embodiments to consisting only of the recited features, and such embodiments may also include features / structures not specifically recited.

[0014] All standards referred to herein are to the latest available revisions unless otherwise stated.

[0015] The present invention discloses a method for the preparation of an electrotechnical fluid composition, an electrotechnical fluid composition, and uses of the electrotechnical fluid composition.

[0016] More particularly, the present invention discloses a process for the preparation of electrotechnical fluid compositions comprising ketonization of renewable feedstocks and hydroprocessing, e.g., hydrodeoxygenation and isomerization, to obtain renewable paraffinic intermediate products, followed by fractionation, preferably by distillation.

[0017] In one embodiment, the resulting renewable paraffinic intermediate product is subjected to at least one fractionation process to recover a hydrocarbon composition having a boiling point range (EN ISO 3405:2011) in the range of about 280° C. to about 400° C. This wider range has the advantage that more cuts can be used, i.e., better yields can be achieved.

[0018] In one embodiment, the resulting renewable paraffinic intermediate product is subjected to at least one fractionation process to recover a hydrocarbon composition having a boiling point range (EN ISO 3405:2011) in the range of about 280°C to about 375°C.

[0019] In one embodiment, the resulting renewable paraffinic intermediate product is subjected to at least one fractional distillation process to recover a hydrocarbon composition having a boiling point range (EN ISO 3405:2011) in the range of about 280° C. to about 350° C. This narrower range has the advantage that the product has better properties than when a wider distillation temperature range is used.

[0020] The present invention also relates to an electrotechnical fluid that meets the requirements according to IEC 60296 (2012), and which electrotechnical composition can be prepared by the method according to the invention.

[0021] The requirement according to IEC60296(2012) is 895kg / m 3 Maximum density at 20℃, maximum pour point at -40℃, 12mm 2 Maximum kinematic viscosity at 40°C of 1800mm / s 2 / s, a minimum flash point of 135°C, a maximum total sulfur content of 500mg / kg, a maximum total acidity of 0.3mgKOH / g, a maximum water content (bulk) of 30mg / kg, and a minimum interfacial tension of 40nMm.

[0022] Furthermore, the invention relates to the use of electrotechnical fluids.

[0023] Renewable paraffin intermediate products can be obtained by ketonization of renewable (biologically derived) raw materials, i.e., renewable feedstocks, and hydroprocessing, such as hydrodeoxygenation and isomerization. Renewable feedstocks have a carbon number distribution ranging from C4 to C26, mainly including C16 and C18. The renewable paraffin intermediate products thus obtained have a carbon number distribution ranging from C4 to C51, mainly including C31 to C35. Renewable paraffin intermediate products mainly include n-paraffins and i-paraffins.

[0024] The distillate obtained after the fractional distillation process to recover a hydrocarbon composition having a boiling point range within the range of about 280° C. to about 400° C. has a carbon number distribution within the range of C15 to C25.

[0025] In one embodiment, renewable paraffinic intermediate products for separation / fractionation are provided by catalytic ketonization and catalytic hydrotreating of renewable feedstocks.

[0026] In another embodiment, hydrotreating comprises catalytic hydrodeoxygenation and hydroisomerization.

[0027] In another embodiment, the separation process comprises fractionation by distillation, which can be continuous or batchwise.

[0028] In one embodiment, the ketonization and hydrotreating steps, such as hydrodeoxygenation and isomerization, are followed by hydrofinishing.

[0029] The boiling range covers the temperature interval from the initial boiling point IBP, defined as the temperature at which the first drop of distilled product is obtained, to the final boiling point FBP, at which the highest boiling compound evaporates.

[0030] According to one embodiment, the obtained renewable paraffinic intermediate product may be subjected to at least one fractional distillation to obtain the electrotechnical composition, wherein the fractional distillation is carried out such that the recovered electrotechnical fluid composition has a boiling point range in the range of about 280°C to about 400°C (EN ISO3405:2011).

[0031] According to one embodiment, the obtained renewable paraffinic intermediate product may be subjected to at least one fractional distillation to obtain the electrotechnical composition, wherein the fractional distillation is carried out such that the recovered electrotechnical fluid composition has a boiling point range in the range of about 280°C to about 375°C (EN ISO3405:2011).

[0032] According to one embodiment, the obtained renewable paraffinic intermediate product may be subjected to at least one fractional distillation to obtain an electrotechnical fluid composition, the fractional distillation being carried out so that the recovered electrotechnical fluid composition has a boiling point range in the range of about 280°C to about 350°C (EN ISO3405:2011).

[0033] In one embodiment, at least one fraction is obtained by distillation.

[0034] The electrotechnical compositions obtained by the disclosed method meet the requirements for such products according to the international standard IEC 60296 (2012).

[0035] The EN ISO 3405:2011 and ASTM D86:2015 standards, "Standard Test Method for Distillation of Petroleum Products and Liquid Fuels at Atmospheric Pressure," and the ASTM D7345:2017 standard, "Standard Test Method for Distillation of Petroleum Products and Liquid Fuels at Atmospheric Pressure (Micro Distillation Method)," describe distillation methods for measuring the boiling point distribution of liquid fuel products with a boiling point range between 0 °C and 400 °C (ASTM D7345: 20 °C to 400 °C). Using ASTM D86 or ASTM D7345, boiling points are measured at 25 vol-% distillation. Boiling points are sometimes reported at 88% distillation.

[0036] Process Description The term "ketonization" refers to the ketonization reaction of carboxylic acids and their derivatives, especially fatty acids, corresponding esters, alcohols, aldehydes, and anhydrides. In this reaction, functional groups react with each other to produce ketones. The ketonization reaction of two carboxylic acids produces a ketone via an anhydride intermediate, with water and carbon dioxide being liberated during the reaction. In the case of alcohols and esters, the ketonization reaction proceeds via an aldehyde to a Tishchenko ester and then to a ketone, and in the case of aldehydes, via a Tishchenko ester to a ketone. In these last two reactions, carbon monoxide is liberated.

[0037] The term "hydrotreatment" refers to the catalytic treatment of organic materials with molecular hydrogen. Preferably, hydrotreating removes oxygen from organic oxygen compounds as water, i.e., by hydrodeoxygenation (HDO). Additionally / alternatively, hydrotreating removes sulfur from organic sulfur compounds as hydrogen sulfide (HS), i.e., by hydrodesulfurization (HDS), nitrogen from organic nitrogen compounds as ammonia (NH), i.e., by hydrodenitrogenation (HDN), halogens, e.g., chlorine, from organic chlorine compounds as hydrochloric acid (HCl), i.e., by hydrodechlorination (HDCl), and / or aromatics to obtain aromatic-free products, i.e., by hydrodearomatization (HDA).

[0038] "Hydrodearomatization" (HDA) refers to the saturation or ring-opening of aromatics with molecular hydrogen under the influence of a catalyst.

[0039] The term "hydrodeoxygenation" (HDO), for example of triglycerides or other fatty acid derivatives or fatty acids, refers to the removal of, for example, carboxyl oxygen as water by molecular hydrogen under the influence of a catalyst.

[0040] Suitable reaction conditions and catalysts for the hydrodeoxygenation of renewable feedstocks and the resulting isomerization of n-paraffins are known, and examples of such processes are shown in FI Patent No. 100248, Examples 1-3, and WO 2015 / 101837.

[0041] The term "deoxygenation" refers to the removal of oxygen from organic molecules, such as fatty acid derivatives, alcohols, ketones, aldehydes and / or ethers, by any of the means mentioned above, or by decarboxylation or decarbonylation.

[0042] The term "isomerisation" refers to a process by which a molecule is changed into another molecule with all the same atoms but in a different arrangement. In this context, isomerisation refers to both the isomerisation and hydroisomerisation of paraffinic carboxylic acids and their alkyl esters.

[0043] The term "intermediate product" refers to a composition obtained from a feedstock after at least one process step, such as ketonization and hydrotreating, but which is further subjected to additional process steps, such as fractionation, to obtain a final product.

[0044] In the process of the present invention, renewable feedstocks are subjected to ketonization and hydrotreating, preferably hydrodeoxygenation and isomerization. When unsaturated carboxylic acids and / or esters of unsaturated carboxylic acids, preferably fatty acids and / or fatty acid alkyl esters, are used as feedstocks, isomerization may be carried out before ketonization followed by hydrodeoxygenation, or isomerization may be carried out after or simultaneously with the ketonization and hydrodeoxygenation steps.

[0045] In one embodiment, the ketonization, hydrodeoxygenation and isomerization steps are followed by hydrofinishing.

[0046] renewable feedstock Renewable feedstock (i.e., biogenic feedstock) refers to a feedstock derived from biological raw materials, including oils and / or fats that typically contain lipids (e.g., fatty acids or glycerides), such as plant oils / fats, vegetable oils / fats, animal oils / fats, fish oils / fats, and algal oils / fats, or oils / fats from other microbial processes, such as genetically engineered algal oils / fats, genetically engineered oils / fats from other microbial processes, and genetically engineered plant oils / fats. Preferably, it is a waste or residual material. Components or derivatives of such materials, such as alkyl esters (typically C1-C5 alkyl esters, e.g., methyl, ethyl, propyl, isopropyl, butyl, sec-butyl esters, etc.) or olefins, can also be used.

[0047] Renewable oils and / or fats can include a single type of oil, a single type of fat, a mixture of different oils, a mixture of different fats, a mixture of oils and fats, fatty acids, glycerol, and / or mixtures of the above.

[0048] These oils and / or fats typically contain C8 to C24 fatty acids and their derivatives, including esters of fatty acids, glycerides, i.e., glycerol esters of fatty acids, which may include monoglycerides, diglycerides, and triglycerides, among others.

[0049] 14 The C-isotope content can be used as evidence of the renewable or biological origin of a feedstock or product. Carbon atoms in renewable materials contain a greater number of unstable radiocarbons ( 14 C) contains atoms. Therefore, 12 C and 14By analyzing the C isotope ratio, it is possible to distinguish carbon compounds derived from biological sources from those derived from fossil sources. Therefore, the specific ratio of the isotopes can be used to identify renewable carbon compounds and distinguish them from non-renewable, i.e., fossil, carbon compounds. The isotope ratio does not change during chemical reactions. An example of a suitable method for analyzing carbon content derived from biological sources is ASTM D6866 (2020). An example of how to apply ASTM D6866 to measure the renewable content of fuels is described in Dijs et al., Radiocarbon, 48(3), 2006, pp. 315-323. For purposes of the present invention, a carbon-containing material, such as a feedstock or product, is considered to be of biological, i.e., renewable, origin if it contains 90% or more modern carbon (pMC), e.g., 100% modern carbon, as measured using ASTM D6866.

[0050] In one embodiment, the electrotechnical fluid composition of the present invention has a modern carbon content (pMC) of at least 5%, in particular at least 60%, such as at least 75% or even 100%.

[0051] Preparation of renewable paraffinic intermediates Generally, renewable paraffinic intermediate products can be produced from renewable feedstocks using any known method. Specific examples of methods for producing renewable paraffinic intermediate products are described in EP 1 963 461 A1.

[0052] In one embodiment, the renewable feedstock comprises fatty acids or fatty acid derivatives, such as triglycerides, or combinations thereof.

[0053] ketonization The preparation of renewable paraffinic intermediate products according to the present invention involves the ketonization of a renewable feedstock. Process conditions for ketonization are known, for example, from EP 1963461 A1. For example, ketonization can be carried out using a metal oxide catalyst. Typical metals include Na, Mg, K, Ca, Sc, Cr, Mn, Fe, Co, Ni, Cu, Zn, Sr, Ti, Y, Zr, Mo, Rh, Cd, Sn, La, Pb, Bi, and rare earth metals. These metal oxides may be supported on a carrier, typical carriers being laterite, bauxite, titanium dioxide, silica, and / or aluminum oxide. The catalyst is preferably a metal oxide catalyst selected from the list consisting of one or more of Ti-, Mn-, Mg-, Ca-, and Zr-containing metal oxide catalysts. The ketonization catalyst more preferably comprises TiO2. The ketonization catalyst is most preferably TiO2, optionally supported on a carrier. For example, the catalyst may have an average pore diameter of 80 to 160 Å and / or a pore size of 40 to 140 μm. 2 / g BET area and / or 0.1-0.3 cm 3 The TiO2 may be in the anatase form with a porosity of 1 / g.

[0054] The ketonization can be carried out, for example, at a pressure of 0.1 to 5 MPa, preferably 0.1 to 1 MPa, while the temperature can range from 100 to 500°C, preferably 100 to 400°C, and more preferably 300 to 400°C. The ketonization can be carried out at a feed flow rate (WHSV) of 0.1 to 10 l / h, preferably 0.3 to 5 l / h, and more preferably 0.3 to 3 l / h. The ketonization reaction can be carried out in the presence of an inert gas, such as nitrogen, or a gas such as hydrogen or carbon dioxide. Preferably, the gas is selected from one or more of CO2, H2, N2, CH4, and HO. Most preferably, it is CO2. The amount can vary from a large excess to a small stoichiometric excess. Preferably, for cost reasons, the gas flow rate is in the range of a 0.1 to 1.5 gas / feed ratio (w / w).

[0055] Hydrotreating Ketonization is followed by hydrotreating, in which the ketonized feed is subjected to hydrogen under pressure in the presence of a catalyst, preferably at least one catalyst selected from Ni, Mo, Co, or W. Typically, hydrotreating removes unsaturated bonds, e.g., double bonds, oxygen (deoxygenation), and other heteroatoms, such as nitrogen, sulfur, and chlorine. Hydrotreating can be selectively carried out in several steps using various catalysts and tailored reaction conditions.

[0056] Hydrodeoxygenation Following ketonization, hydroprocessing, preferably including hydrodeoxygenation (HDO), can be performed, in which oxygen bonds are hydrogenated and the oxygen is removed as HO. Hydrodeoxygenation process conditions are known in the art. For example, hydrodeoxygenation of renewable feedstocks can be performed over a metal sulfide catalyst. The metal can be one or more Group VI metals, such as Mo or W, or one or more non-noble Group VIII metals, such as Co or Ni, or a mixture thereof. The catalyst can be supported on any suitable support, such as alumina, silica, zirconia, titania, amorphous carbon, molecular sieves, or a combination thereof. Typically, the metals are impregnated or deposited on the support as metal oxides. They are then typically converted to their sulfides. Examples of typical catalysts for hydrodeoxygenation include molybdenum-containing catalysts supported on alumina or silica, NiMo, CoMo, or NiW catalysts, although many other hydrodeoxygenation catalysts are known in the art and have been described in conjunction with or in comparison to NiMo and / or CoMo catalysts. Hydrodeoxygenation is preferably carried out in the presence of hydrogen gas under the influence of a sulfided NiMo or sulfided CoMo catalyst.

[0057] The hydrodeoxygenation can be carried out at temperatures between 150°C and 400°C, preferably between 200°C and 400°C, under a hydrogen pressure of 1 to 15 MPa, and a WHSV in the range of 0.5 to 3 1 / h. During the hydrodeoxygenation step using a sulfided catalyst, the sulfided state of the catalyst can be maintained by adding sulfur to the gas phase or by using a feedstock comprising sulfur-containing mineral oil mixed with a renewable feedstock. The sulfur content of the total feed subjected to hydrodeoxygenation can be, for example, in the range of 50 wppm (ppm by weight) to 20,000 wppm, e.g., 50, 100, 500, 1000, 1500, 2000, 2500, 3000, 3500, 4000, 4500, 5000, 5500, 6000, 6500, 7000, 7500, 8000, 8500, 9000, 9500, 10000, 10500 , 11000, 11500, 12000, 12500, 13000, 13500, 14000, 14500, 15000, 15500, 16000, 16500, 17000, 17500, 18000, 18500, 19000, 19500 or 20000 wppm, preferably in the range of 50 wppm to 1000 wppm, more preferably in the range of 50 wppm to 570 wppm.

[0058] Effective conditions for hydrodeoxygenation can reduce the oxygen content of the feedstock to less than 1 wt-%, e.g., less than 0.5 wt-%, or less than 0.2 wt-%, e.g., 0.2-0.05 wt-%, down to essentially oxygen-free conditions, etc. In some cases, conditions can be selected to result in partial hydrodeoxygenation, corresponding to at least 40 wt-%, at least 50 wt-%, or at least 75 wt-% deoxygenation.

[0059] In a preferred embodiment, the hydrodeoxygenation reaction conditions include one or more of the following: a temperature in the range of 250-400°C; a pressure in the range of 2-8 MPa; a WHSV in the range of 0.1-10 l / h, preferably 0.3-5 l / h, more preferably 0.5-3 l / h; and an H2 flow of 350-900 nL H2 / L feed. The hydrodeoxygenation reaction is carried out in the presence of a hydrodeoxygenation catalyst such as Pd, Pt, Ni, NiMo, CoMo, or NiW metal on activated carbon, alumina, and / or silica support, preferably NiMo on an alumina support.

[0060] isomerization The renewable paraffinic intermediate product of the present invention may be provided by subjecting at least the linear hydrocarbons in the feedstock subjected to ketonization to an isomerization treatment to prepare the renewable paraffinic intermediate product.

[0061] The isomerization process causes branching of the hydrocarbon chains of the ketonized and hydrotreated feedstock, i.e., isomerization. The branching of the hydrocarbon chains improves low temperature properties, i.e., the isomer composition formed by the isomerization process has superior low temperature properties compared to the ketonized and hydrotreated feedstock.

[0062] The isomerization step can be carried out in the presence of an isomerization catalyst, optionally in the presence of hydrogen added to the isomerization process. Suitable isomerization catalysts include molecular sieves and / or metals selected from Group VIII of the periodic table, and optionally a support. Preferably, the isomerization catalyst comprises SAPO-11 or SAPO-41, ZSM-22 or ZSM-23, or fernerite, Pt, Pd, or Ni, and Al2O3 or SiO2. Typical isomerization catalysts are, for example, Pt / SAPO-11 / Al2O3, Pt / ZSM-22 / Al2O3, Pt / ZSM-23 / Al2O3, and Pt / SAPO-11 / SiO2. The catalysts may be used alone or in combination. The presence of additional hydrogen is particularly preferred to reduce catalyst deactivation. In a preferred embodiment, the isomerization catalyst is a noble metal bifunctional catalyst, such as Pt-SAPO and / or Pt-ZSM catalyst, and is used in combination with hydrogen. The isomerization step can be carried out, for example, at a temperature of 200 to 400°C, preferably 280 to 400°C, and at a pressure of 1 to 15 MPa, preferably 1 to 10 MPa. The isomerization step can include further intermediate steps, such as a purification step and a fractional distillation step. The isomerization can be carried out, for example, at a temperature of 300 to 350°C.

[0063] In one embodiment, the isomerization reaction conditions include one or more of the following: a temperature in the range of 250-400°C; a pressure in the range of 3-6 MPa; a WHSV in the range of 0.5-3 l / h; and an H2 flow of 100-800 nL H2 / L feed. The hydroisomerization reaction is carried out in the presence of an isomerization catalyst, such as a catalyst comprising a Group VIII metal and a molecular sieve, optionally supported on an alumina and / or silica support.

[0064] Incidentally, isomerization is a process that primarily acts to isomerize the hydrotreated feedstock. That is, while HDO typically results in a small degree of isomerization (usually less than 5 wt-%) depending on the reaction conditions selected, the isomerization process that can be employed in the present invention is one that results in a significant increase in the isoparaffin content.

[0065] The cuts according to the invention have a pour point below -40°C and in that respect must have a very high degree of isomerization, for example at least 90%, preferably at least 95%. Different processes, even from the same cut, will therefore give different products with differences in carbon chain distribution, branching and properties.

[0066] The hydrodeoxygenation and isomerization steps may be carried out simultaneously or sequentially, and may be carried out in a single step on the same catalyst bed using a single catalyst for the combined steps, such as NiW, or a Pt catalyst, such as Pt / SAPO, in a mixture with a Mo catalyst supported on a support, such as NiMo on alumina.

[0067] Hydrofinishing process After the hydrodeoxygenation and isomerization steps, the feedstock may be subjected to hydrofinishing to remove any remaining double bonds and aromatics, but this step is not required. Hydrofinishing can be carried out using hydrogen in the presence of a catalyst at a pressure ranging from 1 to 20 MPa, preferably from 2 to 15 MPa, and particularly preferably from 3 to 10 MPa. The temperature can be in the range of 50 to 500°C, preferably from 200 to 400°C, and particularly preferably from 200 to 300°C. In hydrofinishing, specific catalysts containing metals from Group VIII of the Periodic Table and supports can be used. The hydrofinishing catalyst is preferably a supported Pd, Pt, or Ni catalyst, and the support is alumina and / or silica. Alternatively, finishing can be carried out by removing polar components using an adsorbent such as clay or molecular sieve.

[0068] Fractional distillation process Any known fractionation method, or combination of fractionation methods, may be used in the production of the electrotechnical fluid composition according to the invention from the renewable paraffinic intermediate product to recover a hydrocarbon composition having a boiling point range in the range of about 280°C to about 400°C (EN ISO 3405:2011), or in the range of about 280°C to about 350°C (EN ISO 3405:2011).

[0069] Preferably, the separation is selected such that the carbon number distribution in the fraction boiling in the range of 280 to 400°C is such that the distillate contains 0 to 4 wt% C15 paraffins, 18 to 21 wt% C16 paraffins, 10 to 13 wt% C17 paraffins, 9 to 11 wt% C18 paraffins, 8.5 to 10.5 wt% C19 paraffins, 8.5 to 10.5 wt% C20 paraffins, 8 to 10 wt% C21 paraffins, 7.5 to 9.5 wt% C22 paraffins, 7 to 9.5 wt% C23 paraffins, 6 to 8 wt% C24 paraffins, and 4.5 to 6.5 wt% C25 to C29 paraffins.

[0070] Preferably, the separation is selected such that the carbon number distribution in the fraction boiling between 280 and 350°C is such that the distillate contains 0 to 5 wt-% C15 paraffins, 27 to 30 wt-% C16 paraffins, 16.5 to 19 wt-% C17 paraffins, 15.5 to 18.5 wt-% C18 paraffins, 15.5 to 18 wt-% C19 paraffins, 11.5 to 14.5 wt-% C20 paraffins, 2.5 to 5.5 wt-% C21 paraffins, and 0.1 to 2 wt-% C22 paraffins.

[0071] The carbon number distribution specified above does not exclude other carbon numbers from being present, but these are preferably present in amounts of less than 0.3 wt% at each carbon number.

[0072] Preferably, the separation is selected so that the majority of the i-paraffins are in the distillation fraction recovered.

[0073] In one embodiment, the electrotechnical fluid composition is produced by subjecting a renewable paraffinic intermediate product to at least one separation process comprising distillation.

[0074] In one embodiment, the initial boiling point IBP is 280° C. and the final boiling point FBP is 400° C. (EN ISO3405:2011).

[0075] In one embodiment, the initial boiling point IBP is 280° C. and the final boiling point FBP is 375° C. (EN ISO3405:2011).

[0076] In one embodiment, the initial boiling point IBP is 280° C. and the final boiling point FBP is 350° C. (EN ISO3405:2011).

[0077] In one embodiment, the process comprises two or more separation steps.

[0078] Selection of renewable feedstocks for favorable properties, such as selecting renewable feedstocks with high amounts of compounds with carbon chain lengths peaking at C16 and C18, can be used to increase the yield of electrotechnical fluid compositions and products containing renewable base oils.

[0079] The yield of the electrotechnical fluid composition can also be improved by the selection of process conditions in the renewable paraffinic intermediate production process.

[0080] In one embodiment of the present invention according to FIG. 1, a feedstock containing free fatty acids and glycerol is subjected to ketonization under ketonization conditions and then hydrodeoxygenated under hydrodeoxygenation conditions. The ketonized and hydrodeoxygenated feedstock is then subjected to isomerization, followed by an optional hydrofinishing step. The product is then subjected to an initial fractionation, e.g., distillation or stripper, where it is fractionated into demister naphtha, stripper naphtha, and a bottoms product. The stripper naphtha is further fractionated to result in middle distillates, e.g., diesel, and gasoline for use with gasoline obtained from the demister naphtha. The bottoms product is further fractionated into middle distillates, e.g., diesel, and a renewable base oil fraction. The renewable base oil fraction is further fractionated, and distillation cuts between 280 and 400°C or 280 and 350°C are collected and evaluated for performance as electrotechnical fluid compositions. Heavier cuts include renewable base oil products.

[0081] In one embodiment, the present invention relates to a method for producing an electrotechnical fluid composition, the method comprising the steps of: subjecting a renewable feedstock comprising free fatty acids and glycerides to ketonization under ketonization conditions; subjecting the ketonized renewable feedstock to hydrotreating under hydrotreating conditions to obtain renewable paraffinic intermediate products; and subjecting the renewable paraffinic intermediate products to at least one fractional distillation to obtain an electrotechnical fluid composition, wherein the electrotechnical fluid composition meets the requirements according to the IEC 60296 (2012) international standard.

[0082] In one embodiment, the electrotechnical fluid composition has a viscosity of 895 kg / m 3 Less than 800 kg / m 3 It has the following density at 20°C:

[0083] In one embodiment, the electrotechnical fluid composition has a pour point (ISO 3016) of less than -40°C.

[0084] In one embodiment, the electrotechnical fluid composition comprises a 12 mm 2 / s or less, preferably 10 mm 2 / s or less, preferably 8 mm 2 / s or less, e.g. 6 mm 2 It has a kinematic viscosity of 1 / s or less at 40°C.

[0085] In one embodiment, the electrotechnical fluid composition comprises an 1800mm 2 / s or less, preferably 150 mm 2 / s or less, e.g., 120 mm 2 The kinematic viscosity at -30°C is equal to or less than 1 / s.

[0086] In one embodiment, the electrotechnical fluid composition has a flash point of 135°C or greater.

[0087] In one embodiment, the electrotechnical fluid composition has a total acidity of 0.01 mg KOH / g or less, such as 0.005 mg KOH / g or less.

[0088] In one embodiment, the electrotechnical fluid composition has a water content of 30 mg / kg or less, preferably 20 mg / kg or less.

[0089] In one embodiment, the at least one fractional distillation is carried out in such a way that the recovered electrotechnical composition has a boiling point range in the range of about 280°C to about 400°C, preferably in the range of about 280°C to about 400°C (EN ISO 3405:2011), more preferably in the range of about 280°C to about 350°C (EN ISO 3405:2011).

[0090] In one embodiment, the at least one fraction is provided by distillation.

[0091] In one embodiment, the at least one fraction is provided by fractional distillation.

[0092] In one embodiment, the ketonization is carried out at a temperature in the range of 100 to 500°C, preferably 100 to 400°C, more preferably 300 to 400°C.

[0093] In one embodiment, the ketonization is carried out at a pressure of 0.1 to 5 MPa, preferably 0.1 to 1 MPa.

[0094] In one embodiment, the ketonization is carried out at a feed flow rate WHSV of 0.1 to 10 l / h, preferably 0.3 to 5 l / h, more preferably 0.3 to 3 l / h.

[0095] In one embodiment, the ketonization is carried out in the presence of at least one metal oxide ketonization catalyst.

[0096] In one embodiment, the metal oxide ketonization catalyst comprises Ti, more preferably TiO2, and even more preferably the catalyst consists of TiO2.

[0097] In one embodiment, the ketonization conditions include a temperature of 100-400° C., a pressure of 0.1-5 MPa, and the presence of a metal oxide ketonization catalyst, wherein the ketonization catalyst preferably comprises TiO 2 .

[0098] In one embodiment, the hydrotreating conditions include the presence of hydrogen gas and at least one catalyst selected from Ni, Mo, Co, or W.

[0099] In one embodiment, the hydrotreating comprises simultaneous or sequential hydrodeoxygenation under hydrodeoxygenation conditions and isomerization under isomerization conditions.

[0100] In one embodiment, the hydrodeoxygenation is carried out at a temperature in the range of 150 to 400°C, preferably 200 to 400°C.

[0101] In one embodiment, the hydrodeoxygenation reaction is carried out at a pressure of 1 to 15 MPa, preferably 2 to 8 MPa.

[0102] In one embodiment, the hydrodeoxygenation is carried out at a feed flow rate WHSV of 0.1 to 10 1 / h, preferably 0.3 to 5 1 / h, more preferably 0.5 to 3 1 / h.

[0103] In one embodiment, the hydrodeoxygenation reaction is carried out at an H2 flow rate of 350-900 nl H2 / l feed.

[0104] In one embodiment, the hydrodeoxygenation is carried out in the presence of at least one hydrodeoxygenation catalyst.

[0105] In one embodiment, the hydrodeoxygenation catalyst comprises at least one metal selected from the group consisting of Pd, Pt, Ni, CoMo, NiMo, NiW, and CoNiMo.

[0106] In one embodiment, the catalyst may be supported on a support selected from the group consisting of alumina, silica, zirconia, titania, amorphous carbon, molecular sieves, or combinations thereof.

[0107] In one embodiment, the hydrodeoxygenation conditions comprise a hydrogen pressure in the range of 1 to 15 MPa at a temperature in the range of 150 to 400°C and the presence of a catalyst comprising Pd, Pt, Ni, NiMo, CoMo or NiW metal and an activated carbon, alumina and / or silica support.

[0108] In one embodiment, the isomerization conditions include a temperature range of 200 to 400°C, preferably 250 to 400°C, and more preferably 280 to 400°C.

[0109] In one embodiment, the isomerization conditions include a pressure of 1 to 15 MPa, preferably 1 to 10 MPa.

[0110] In one embodiment, the isomerization conditions include a feed flow rate WHSV of 0.5 to 3 1 / h.

[0111] In one embodiment, the isomerization conditions include an H2 flow of 100 to 800 nl H2 / l feed.

[0112] In one embodiment, the isomerization conditions comprise the presence of a hydroisomerization catalyst.

[0113] In one embodiment, the hydroisomerization catalyst is selected from Group VIII metals, preferably Pd, PT or Ni, optionally supported on an alumina and / or silica support.

[0114] In one embodiment, the isomerization conditions comprise a hydrogen pressure in the range of 1 to 15 MPa at a temperature in the range of 200 to 400°C, and the presence of a catalyst selected from molecular sieves, and Pd, Pt or Ni metal, and / or a support, wherein the support is alumina and / or silica.

[0115] In one embodiment, the method further comprises subjecting the renewable paraffinic intermediate product to a second or further, e.g., third, fractionation to obtain a renewable base oil product meeting API Group III base oil specifications of greater than 90 wt. % saturated hydrocarbons, less than 0.03 wt. % sulfur, and a viscosity index greater than 120.

[0116] In one embodiment, the present invention relates to an electrotechnical fluid composition, or an electrotechnical fluid composition obtainable by the method according to the present invention, which contains more than 95 wt-%, preferably more than 97 wt-%, even more preferably more than 99 wt-%, based on the total weight of the composition, of paraffins in the range C15 to C29, preferably in the range C15 to C25, and which electrotechnical composition meets the requirements according to IEC 60296.

[0117] The following embodiments apply both to electrotechnical fluid compositions and to electrotechnical fluid compositions obtainable by the method according to the invention.

[0118] In one embodiment, the electrotechnical fluid composition has a viscosity of 895 kg / m 3 Less than 800 kg / m 3 It has a density at 20°C that is less than or equal to

[0119] In one embodiment, the electrotechnical fluid composition has a pour point (ISO 3016) of less than -40°C.

[0120] In one embodiment, the electrotechnical fluid composition comprises a 12 mm 2 / s or less, preferably 10 mm 2 / s or less, preferably 8 mm 2 It has a kinematic viscosity of 1 / s or less at 40°C.

[0121] In one embodiment, the electrotechnical fluid composition comprises an 1800mm 2 / s or less, preferably 150 mm 2 / s or less at -30°C.

[0122] In one embodiment, the electrotechnical fluid composition has a flash point of 135°C or greater.

[0123] In one embodiment, the electrotechnical fluid composition has a total acidity of 0.01 mg KOH / g or less.

[0124] In one embodiment, the electrotechnical fluid composition has a water content of 30 mg / kg or less, preferably 20 mg / kg or less.

[0125] In one embodiment, the electrotechnical composition comprises more than 0.01 wt-%, preferably more than 2.5 wt-%, but up to 5 wt-%, C15 paraffin, based on the total weight of the composition.

[0126] In one embodiment, the electrotechnical composition comprises more than 5 wt-%, preferably more than 18 wt-%, even more preferably more than 20 wt-%, more preferably more than 25 wt-%, for example more than 28 wt-%, but up to 35 wt-%, of C16 paraffins, based on the total weight of the composition.

[0127] In one embodiment, the electrotechnical composition comprises more than 5 wt-%, preferably more than 10 wt-%, more preferably more than 15 wt-%, even more preferably more than 17 wt-%, but up to 24 wt-%, of C17 paraffin, based on the total weight of the composition.

[0128] In one embodiment, the electrotechnical composition comprises more than 5 wt-%, preferably more than 8 wt-%, preferably more than 15 wt-%, more preferably more than 16 wt-%, but up to 23 wt-%, of C18 paraffins, based on the total weight of the composition.

[0129] In one embodiment, the electrotechnical composition comprises more than 5 wt-%, preferably more than 8 wt-%, preferably more than 15 wt-%, more preferably more than 16 wt-%, but up to 23 wt-%, of C19 paraffins, based on the total weight of the composition.

[0130] In one embodiment, the electrotechnical composition comprises more than 5 wt-%, preferably more than 8 wt-%, more preferably more than 9 wt-%, even more preferably more than 12 wt-%, but not more than 19 wt-% C20 paraffins, based on the total weight of the composition.

[0131] In one embodiment, the electrotechnical composition comprises less than 12 wt-%, preferably less than 10 wt-%, more preferably less than 9 wt-%, even more preferably less than 5 wt-%, but at least 1 wt-% C21 paraffins, based on the total weight of the composition.

[0132] In one embodiment, the electrotechnical composition comprises less than 12 wt-%, preferably less than 10 wt-%, more preferably less than 9 wt-%, even more preferably less than 1 wt-%, but at least 0.1 wt-%, of C22 paraffins, based on the total weight of the composition.

[0133] In one embodiment, the electrotechnical composition comprises less than 14 wt-%, preferably less than 10 wt-%, more preferably less than 9 wt-%, even more preferably less than 1 wt-%, even more preferably less than 0.25 wt-%, but at least 0.05 wt-% C23 paraffins, based on the total weight of the composition.

[0134] In one embodiment, the electrotechnical composition comprises less than 8 wt-%, preferably less than 7 wt-%, more preferably less than 0.5 wt-%, and even more preferably less than 0.1 wt-% C24 paraffins, based on the total weight of the composition.

[0135] In one embodiment, the total isoparaffin content of the electrotechnical fluid composition is greater than 93 wt-% but less than 99 wt-%, preferably greater than 94 wt-% but less than 98 wt-%, and more preferably greater than 95 wt-% but less than 97 wt-%, based on the total weight of the composition.

[0136] In one embodiment, the weight ratio of the amount of i-paraffins to the amount of n-paraffins is greater than 20, based on the total weight of the composition.

[0137] In one embodiment, the weight ratio of the amount of i-paraffins to the amount of n-paraffins is less than 32, based on the total weight of the composition.

[0138] In one embodiment, the electrotechnical fluid has a viscosity of 12 mm, measured according to ENISO 3104. 2 / s or less, typically 3-4.5 mm 2 Maximum kinematic viscosity at 40°C between 1800mm / s, measured according to ENISO 3104 2 / s or less, typically 120 mm 2 / s, a flash point (PM) measured in accordance with ENISO 2719 of 135°C or greater, typically at least 137°C, and an acidity of 0.3 mg KOH / g or less, typically less than 0.009 mg KOH / g.

[0139] In one embodiment, the electrotechnical fluid has a viscosity of 12 mm, measured according to ENISO 3104. 2 / s or less, typically 4-8 mm 2 Maximum kinematic viscosity at 40°C between 1800mm / s, measured according to ENISO 3104 2 / s or less, typically 500 mm 2 / s, a flash point (PM) measured in accordance with ENISO 2719 of at least 135°C, typically at least 135°C, and an acidity of 0.3 mg KOH / g or less, typically 0.002 mg KOH / g or less.

[0140] In one embodiment, the electrotechnical composition has a carbon number range up to C29.

[0141] In one embodiment, the electrotechnical composition has a carbon number range up to C25.

[0142] In one embodiment, the electrotechnical composition has a carbon number range up to C15.

[0143] In one embodiment, the present invention relates to the use of the electrotechnical fluid composition according to the invention in a transformer, preferably a power transformer.

[0144] In one embodiment, the present invention relates to the use of the electrotechnical fluid composition according to the present invention as a transformer oil or as a component of a transformer oil, battery coolant, heat transfer fluid, coolant, insulating oil, shock absorbing fluid or cable oil.

[0145] In one embodiment, the present invention relates to the use of an electrotechnical fluid composition according to the present invention as an electric vehicle battery coolant.

[0146] In one embodiment, the present invention relates to the use of an electrotechnical fluid composition according to the present invention as a server farm coolant.

[0147] In one embodiment, the present invention relates to an electrotechnical fluid composition comprising more than 95 wt-% paraffins in the C15 to C29 range, preferably more than 97 wt-%, even more preferably more than 99 wt-%, based on the total weight of the composition, in the range of C15 to C29, preferably in the range of C15 to C25, wherein the electrotechnical composition meets the requirements according to IEC 60296. [Example]

[0148] Example 1 (Comparative) Table 1 summarizes the physical and chemical properties of the composition of Example 1, NRI-A (comparative).

[0149] Table 2 summarizes the carbon number distribution of the composition of NRI-A in Example 1.

[0150] The sample composition of Example 1 was produced by hydrodeoxygenation and isomerization of a renewable feedstock, as described above. No ketonization was performed prior to hydrodeoxygenation. The isomerization step was followed by a distillation step to recover a hydrocarbon composition having an initial boiling point (IBP) of 275°C and a final boiling point (FBP) of 300°C.

[0151] The carbon number distribution of the composition of Example 1 is shown in Table 2. The composition of Example 1 exhibits a very narrow carbon number distribution, with C15 paraffins comprising 0.02 wt% of the composition, C16 paraffins comprising 2.31 wt% of the composition, C17 paraffins comprising 24.97 wt% of the composition, C18 paraffins comprising 70.65 wt% of the composition, C19 paraffins comprising 1.59 wt% of the composition, C20 paraffins comprising 0.45 wt% of the composition, and C21 paraffins comprising 0.01 wt% of the composition. 99.97 wt% of the total paraffins are in the C16-C20 range.

[0152] [Table 1]

[0153] [Table 2]

[0154] Example 2 (Comparative) Table 3 summarizes the physical and chemical properties of the three commercially available products: Commercial Sample A, Commercial Sample B, and Neste NRI-B (comparison) composition.

[0155] [Table 3]

[0156] Example 3 RBO Process Palm oil fatty acid distillate (PFAD) was used as the feedstock for the ketonization step. The fractionated feed used consisted mainly of C16:0 fatty acids. Ketonization was carried out in a pilot continuous fixed-bed reactor system operated at 350 °C under 1.8 MPa pressure using TiO2 catalyst in a CO2 atmosphere (650 L / h). The feed rate was 2.2 kg / h with a gas ratio of 0.6 g / g and a WHSV of 1.1 l / h. The product gas was separated from the liquid ketone product and introduced into a continuous fixed-bed HDO reactor containing a NiMo catalyst. The ketone product, which mainly contained C31 ketones, underwent hydrodeoxygenation at 309 °C under 6.0 MPa pressure in hydrogen (1270 L / h) with a feed rate of 1.4 kg / h and a gas ratio of 712 Nl / l. The resulting paraffinic liquid HDO product was further subjected to hydroisomerization and hydrofinishing. The hydroisomerization reactor used a commercial hydroisomerization catalyst and was operated at 340°C under a pressure of 4.5 MPa with a WHSV of 0.9 l / h and a gas (hydrogen) to feed ratio of 674 Nl / l. The temperature of the hydrofinishing reactor was 285°C at the same pressure and a WHSV of 3.0 l / h.

[0157] Recovery of electrotechnical fluids The renewable paraffinic branched intermediate product obtained from the RBO process was fractionated by distillation into demister naphtha, naphtha, diesel, electrotechnical fluid components, and renewable base oil components. Two different electrotechnical fluid components were collected: a distillation cut between 280 and 400 °C and a distillation cut between 280 and 350 °C. These cuts were evaluated in terms of their properties and suitability for electrotechnical applications.

[0158] Evaluation of the properties of the two fractional distillation cuts showed that the distillation cut was well suited for use as an electrotechnical composition.

[0159] Table 4 summarizes the physical and chemical properties of the two electrotechnical compositions of Example 3, distillation cut at 280-400°C or 280-350°C.

[0160] Table 5 summarizes the carbon number distribution of compositions distilled and cut at 280 to 400°C, and Table 6 summarizes the carbon number distribution of compositions distilled and cut at 280 to 350°C.

[0161] [Table 4]

[0162] [Table 5]

[0163] [Table 6]

[0164] In the distillation cut at 280-400°C, 99.78 wt-% of all paraffins were in the C15 to C29 range. Improvements compared to, for example, the electrotechnical composition of Example 1, i.e., NRI-A, could be seen, for example, in the higher degree of isomerization of the product obtained when using the process according to the invention (4.59% normal paraffins in NRI-A of Example 1, compared to 3.21% normal paraffins in the 280-400°C cut according to the invention).

[0165] It was found that in both the 280-400°C and 280-350°C distillation cuts, higher molecular weight components, i.e. even C25-C29, were obtained with the electrotechnical composition according to the invention compared to the composition of Example 1, in which no ketonization was carried out in the preparation process and the higher molecular weight components of the product ended at C20.

[0166] The ratio of the amount of C15 i-paraffin to the amount of C15 n-paraffin was 3.8 based on the weight of C15 i-paraffin and the weight of C15 n-paraffin in the composition. The ratio of the amount of C16 i-paraffin to the amount of C16 n-paraffin was 12.5 based on the weight of C16 i-paraffin and the weight of C16 n-paraffin in the composition. The ratio of the amount of C17 i-paraffin to the amount of C17 n-paraffin was 29.0 based on the weight of C17 i-paraffin and the weight of C17 n-paraffin in the composition. The ratio of the amount of C18 i-paraffin to the amount of C18 n-paraffin was 74.8 based on the weight of C18 i-paraffin and the weight of C18 n-paraffin in the composition. The ratio of the amount of C19 i-paraffin to the amount of C19 n-paraffin was 92.8 based on the weight of C19 i-paraffin and the weight of C19 n-paraffin in the composition. The ratio of the amount of C20 i-paraffins to the amount of C20 n-paraffins was 135.4 based on the weight of C20 i-paraffins and the weight of C20 n-paraffins in the composition. The ratio of the amount of C21 i-paraffins to the amount of C21 n-paraffins was 48.9 based on the weight of C21 i-paraffins and the weight of C21 n-paraffins in the composition. The ratio of the amount of C22 i-paraffins to the amount of C22 n-paraffins was 56.0 based on the weight of C22 i-paraffins and the weight of C22 n-paraffins in the composition. The ratio of the amount of C23 i-paraffins to the amount of C23 n-paraffins was 42.3 based on the weight of C23 i-paraffins and the weight of C23 n-paraffins in the composition. The ratio of the amount of C24 i-paraffins to the amount of C24 n-paraffins was 68.7 based on the weight of C24 i-paraffins and the weight of C24 n-paraffins in the composition.

[0167] For distillations at 280-350°C, 100 wt% of all paraffins were in the C15-C29 range, and 99.92 wt% of all paraffins were in the C15-C22 range. The ratio of the amount of C15 i-paraffins to the amount of C15 n-paraffins was 3.8 based on the weight of C15 i-paraffins and the weight of C15 n-paraffins in the composition. The ratio of the amount of C16 i-paraffins to the amount of C16 n-paraffins was 11.9 based on the weight of C16 i-paraffins and the weight of C16 n-paraffins in the composition. The ratio of the amount of C17 i-paraffins to the amount of C17 n-paraffins was 23.3 based on the weight of C17 i-paraffins and the weight of C17 n-paraffins in the composition. The ratio of the amount of C18 i-paraffin to the amount of C18 n-paraffin was 129.2 based on the weight of C18 i-paraffin and the weight of C18 n-paraffin in the composition. The ratio of the amount of C19 i-paraffin to the amount of C19 n-paraffin was 53.4 based on the weight of C19 i-paraffin and the weight of C19 n-paraffin in the composition. The ratio of the amount of C20 i-paraffin to the amount of C20 n-paraffin was 45.4 based on the weight of C20 i-paraffin and the weight of C20 n-paraffin in the composition. The ratio of the amount of C21 i-paraffin to the amount of C21 n-paraffin was 65.3 based on the weight of C21 i-paraffin and the weight of C21 n-paraffin in the composition. The ratio of the amount of C22 i-paraffins to the amount of C22 n-paraffins was 58.0 based on the weight of C22 i-paraffins and the weight of C22 n-paraffins in the composition.

[0168] As can be seen from the table, the distillation cuts at 280-350°C and 280-400°C were evaluated from the perspective of transformer oil performance and gave good results. The results of both cuts were in line with the specification requirements. The 280-350°C cut had a lower viscosity, a lower cloud point, and a higher interfacial tension than the 280-400°C cut.

[0169] The aromatics content of the 280-350°C fraction was measured according to UOP 495 and was found to be as low as 0.001 wt-% based on the total weight of the composition. Such a low amount is beneficial for safety and toxicity reasons and represents a significant advantage over other electrotechnical compositions with higher aromatics contents. Furthermore, the naphthalene content was measured according to UOP 495 for the 280-350°C fraction and was found to be <0.001, a beneficially low value since naphthalene is a carcinogen.

[0170] It is obvious to a person skilled in the art that with the advancement of technology, the inventive concept of the present invention can be implemented in various ways. The present invention and its embodiments are not limited to the examples described above, but may vary within the scope of the claims.

Claims

1. 1. A method for producing an electrotechnical fluid composition comprising: (a) subjecting a renewable feedstock comprising free fatty acids and glycerides to ketonization under ketonization conditions; (b) subjecting the ketonized renewable feedstock to hydrotreating conditions to obtain a renewable paraffinic intermediate product; (c) subjecting said renewable paraffinic intermediate product to at least one fractionation by distillation to obtain an electrotechnical fluid composition, so that the recovered electrotechnical composition has a boiling point range (EN ISO 3405:2011) in the range of 280°C to 400°C, and of the paraffins obtained, more than 99 wt-% are in the range C15 to C29, based on the weight of the total composition, and the weight ratio of the amount of i-paraffins to the amount of n-paraffins is greater than 20 and less than 32, based on the weight of the total composition. Including, and wherein said recovered electrotechnical fluid composition meets the requirements according to the IEC 60296 (2012) international standard.

2. The ketonization conditions include a temperature of 100 to 500° C., a pressure of 0.1 to 5 MPa, and the presence of a metal oxide ketonization catalyst, wherein the ketonization catalyst is TiO 2 The method of claim 1 , comprising:

3. 3. The process of claim 1 or 2, wherein the hydrotreating conditions include the presence of hydrogen gas and at least one catalyst selected from Ni, Mo, Co, or W.

4. 4. The process of any one of claims 1 to 3, wherein the hydrotreating comprises simultaneous or sequential hydrodeoxygenation under hydrodeoxygenation conditions and isomerization under isomerization conditions.

5. 5. The process of claim 4, wherein the hydrodeoxygenation conditions comprise a hydrogen pressure in the range of 1 to 15 MPa at a temperature in the range of 150 to 400°C and the presence of a catalyst comprising Pd, Pt, Ni, NiMo, CoMo or NiW metal and an activated carbon, alumina and / or silica support.

6. 6. The process of claim 4 or 5, wherein the isomerization conditions comprise a hydrogen pressure in the range of 1 to 15 MPa at a temperature in the range of 200 to 400°C, and the presence of a catalyst selected from molecular sieves, and Pd, Pt or Ni metals, and / or a support, wherein the support is alumina and / or silica.

7. 7. The method of any one of claims 1 to 6, further comprising subjecting the renewable paraffinic intermediate product to at least one fractionation to obtain a renewable base oil product that meets API Group III base oil specifications of greater than 90 wt. % saturated hydrocarbons, less than 0.03 wt. % sulfur, and a viscosity index greater than 120.

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