Hydrocarbon component

Abstract

Disclosed herein is a hydrocarbon component comprising predominantly a C15 to C22 normal paraffin, a C15 to C22 single branched isoparaffin, and a C15 to C22 multi-branched isoparaffin. In the hydrocarbon component, the weight ratio of isoparaffins to n-paraffins is higher than that of hydrocarbon components in the prior art. Due to its improved properties, the hydrocarbon component according to the invention can be used for a wide range of applications, in particular in north grade diesel fuels, where it can be incorporated in higher proportions.

Description

Technical Field

[0001] The present disclosure generally relates to processes for producing fuel components and products thereof. The present disclosure particularly, but not exclusively, relates to a novel hydrocarbon component, primarily a renewable diesel fuel component obtainable from a renewable feedstock. Background Art

[0002] Without admitting that any of the techniques described herein represent prior art, this section presents useful background information.

[0003] There is a continuous need to reduce greenhouse gas emissions and / or carbon footprint, especially in the transportation sector. As a result, interest in renewable transportation fuels and alternatives to various petrochemicals has been growing.

[0004] Processes for producing fuel components from renewable raw materials have been proposed. Non-fossil diesels, such as hydrotreated vegetable oils (HVO), renewable diesel, and in particular fatty acid methyl esters (FAME), have difficulties in meeting requirements for low-temperature properties. Measures to improve low-temperature properties, namely lowering the cloud point (CP) and cold filter plugging point (CFPP) (given as temperature), have been proposed, and winter grades and even arctic grades of at least some non-fossil diesels are now available. However, lowering the CP and / or CFPP usually leads to changes in other product characteristics (such as viscosity, density and / or cetane number) in an undesirable direction. In general, viscosity and low-temperature properties are inversely proportional. For example, commercially available fossil arctic grades of diesel have a relatively low viscosity of less than 2.000 mm² / s at 40°C.

[0005] However, higher viscosity is desirable as it improves fuel injection in the fuel system, as long as the viscosity of the fuel meets the general requirements of the EN590 / EN15940 specification (viscosity max. 4.500 mm² / s at 40°C) or the EN590:2022 Arctic Diesel specification (viscosity max. 4.000 mm² / s at 40°C).

[0006] The need for renewable fuel components with good low temperature properties continues. More specifically, there is a need to provide a hydrocarbon component suitable for Arctic use, having a high cetane number and a viscosity at 40°C higher than conventional fossil Arctic grade diesel. In particular, there is interest in producing a hydrocarbon component that can be used in a wide range of applications, such as in fuels, transformer oils, gear oils, solvents, lubricating oils, heating oils, insulating oils, hydraulic oils and turbine oils or for power generation. Summary of the invention

[0007] It is an object of the present invention to solve or alleviate at least some of the problems associated with the prior art.It is an object to improve the quality of hydrocarbon components, in particular diesel fuel components, obtainable from renewable resources.

[0008] The claims attached to the present invention define the scope of protection. Any examples and technical descriptions of products, processes and / or uses not covered by the claims in the specification and / or drawings are not presented as embodiments of the present invention, but are presented as examples to help understand the present invention.

[0009] According to a first exemplary aspect, there is provided a hydrocarbon component, preferably a renewable hydrocarbon component, such as a diesel fuel component or a renewable diesel fuel component, comprising normal paraffins, monobranched isoparaffins and multi-branched isoparaffins, wherein the total amount of C15-C22 normal paraffins, C15-C22 monobranched isoparaffins and C15-C22 multi-branched isoparaffins is at least 90 wt-%, based on the weight of the total hydrocarbon component, and wherein the weight ratio of C15-C22 isoparaffins to C15-C22 normal paraffins is at least 22:1, preferably at least 24:1, more preferably at least 30:1, even more preferably at least 34:1.

[0010] The inventors have discovered that the hydrocarbon components of the present invention and embodiments thereof have specific advantages over prior art hydrocarbon components, particularly renewable hydrocarbon components (such as prior art renewable diesel components). These advantages relate to, for example, higher density and higher viscosity at temperatures above zero degrees Celsius, while having excellent low temperature properties, including good flow properties at sub-zero temperatures, as discussed in detail below.

[0011] The production of the hydrocarbon component may employ a specific process comprising a combination of hydroisomerization and hydrocracking of a paraffinic feed.The hydrocarbon component of the present invention may be obtained from a process for producing a renewable fuel component, the process further comprising the recovery of at least one aviation fuel component.

[0012] According to a second exemplary aspect, there is provided a diesel fuel composition comprising 1 to 99 vol-%, preferably 10 to 70 vol-% of a hydrocarbon component as defined herein, based on the volume of the total diesel fuel composition. Surprisingly, the hydrocarbon component can comprise a very high volume fraction in the diesel fuel composition, such as 70 vol-%, in particular due to the very high density of the hydrocarbon component of the present invention.

[0013] According to a third exemplary aspect, there is provided use of a hydrocarbon component of the present invention in a diesel fuel composition for improving one or more product properties of the diesel fuel composition.

[0014] According to a fourth exemplary aspect, there is provided a hydrocarbon component as defined herein in a feedstock for an industrial conversion process, preferably a thermal cracking feedstock and / or a catalytic cracking feedstock; in a transformer oil; in a heat transfer medium or media; in a switchgear oil; oil); shock absorber oil; insulating oil; hydraulic fluid; gear oil; transmission fluid; degreasing composition; penetrating oil; anticorrosive composition; multipurpose oil; metalworking fluid; rolling oil (especially for aluminum); cutting oil; drilling fluid; solvent; lubricant; spreading oil; carrier; dispersant composition; demulsifier; extractant; coating composition; coating fluid or paste; adhesive; resin; varnish; printing paste or ink; detergent; cleaning agent; plasticizing oil; turbine oil; hydrophobizing composition; agriculture; crop protection fluid; construction; concrete release formulation; electronics; medical equipment; compositions for the automotive, electrical, textile, packaging, paper, cosmetic and / or pharmaceutical industries, and / or in the manufacture of intermediates therefor. In said uses, the excellent physicochemical properties can be utilized, while the preferred renewable property is valued.

[0015] Various non-binding example aspects and implementations have been described above. The above implementations are only used to explain selected aspects or steps that can be used in different implementations. Some implementations may be presented with reference to only certain example aspects. It should be understood that the corresponding implementations may also be applicable to other example aspects. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Some example embodiments will be described with reference to the accompanying drawings, in which:

[0017] Figure 1 An exemplary embodiment of a process for producing the hydrocarbon component of the present invention is schematically shown.

[0018] Figure 2 Another exemplary embodiment of a process for producing the hydrocarbon component of the present invention is schematically shown. DETAILED DESCRIPTION

[0019] In the following description, the same reference numerals denote the same elements or steps.

[0020] Unless otherwise stated, all standards referred to herein are the latest revised editions available on the filing date.

[0021] Unless otherwise stated, for distillation characteristics such as initial boiling point (IBP), final boiling point (FBP), T5 temperature (5 vol-% recovery), T95 temperature (95 vol-% recovery) and boiling range, reference is made to EN ISO 3405-2019. IBP is the temperature at which the first drop of condensate drips from the lower end of the condenser tube, and FBP is the maximum value of the thermometer reading during the test, which usually occurs after all the liquid at the bottom of the flask has evaporated. For boiling point distribution, reference is also made to the GC-based method (simulated distillation (simdis)) ASTM D2887-19e1, or to ASTM D7096-19 for gasoline range hydrocarbons.

[0022] As used in the context of the present disclosure, a diesel fuel component refers to a hydrocarbon component suitable for use in a fuel composition that complies with a diesel fuel standard specification, such as the specifications set forth in EN 590:2022 or EN 15940:2016 + A1:2018 + AC:2019. Typically, such diesel fuel components have a boiling point (i.e., having an IBP and a FBP) in the range of about 160°C to about 380°C as determined according to EN ISO 3405-2019.

[0023] As used in the context of the present disclosure, an aviation fuel component refers to a hydrocarbon composition suitable for use in a fuel composition that meets the aviation fuel standard specifications (such as the specifications specified in ASTM D7566-21). Typically, such aviation fuel components have a boiling point (i.e., having an IBP and a FBP) in the range of about 100°C to about 300°C, such as in the range of about 150°C to about 300°C, as determined according to EN ISO 3405-2019.

[0024] As used in the context of this disclosure, gasoline fuel component or naphtha refers to a hydrocarbon component suitable for use in a fuel composition that complies with a gasoline fuel standard specification, such as the specifications set forth in 228-2012 + A1-2017. Typically, such gasoline fuel components have a boiling point (i.e., having an IBP and a FBP) in the range of about 25°C to about 210°C as determined according to EN ISO 3405-2019.

[0025] As used in the context of the present disclosure, a bunker fuel component refers to a hydrocarbon component suitable for use in a fuel composition that complies with a standard specification for bunker fuels, such as the specification set forth in ISO 8217-2017. Typically, such bunker fuel components have a boiling point (i.e., having an IBP and a FBP) in the range of about 180°C to about 600°C, such as in the range of about 180°C to about 400°C, as determined according to EN ISO 3405-2019.

[0026] As used herein, hydrocarbon refers to a compound consisting of carbon and hydrogen. Hydrocarbons of particular interest in the context of the present invention include paraffins, normal paraffins, isoparaffins, monobranched isoparaffins, multibranched isoparaffins, olefins, cycloparaffins and aromatic hydrocarbons. In this article, oxygenated hydrocarbons refer to hydrocarbons containing covalently bound oxygen.

[0027] As used herein, paraffins refer to non-cyclic alkanes, i.e., non-cyclic, open-chain saturated hydrocarbons; paraffins may be linear (normal paraffins, n-paraffins) or branched (isoparaffins, i-paraffins). In other words, paraffins herein refer to normal paraffins and / or isoparaffins.

[0028] In the context of the present disclosure, isoparaffin refers to branched open chain alkanes, i.e., non-cyclic, open chain saturated hydrocarbons with one or more alkyl side chains. Herein, isoparaffins with one alkyl side chain or branch are referred to as monobranched isoparaffins, and herein, isoparaffins with two or more alkyl side chains or branches are referred to as multi-branched isoparaffins. In other words, isoparaffins herein refer to monobranched isoparaffins and / or multi-branched isoparaffins. The alkyl side chains of isoparaffins may be, for example, C1-C9 alkyl side chains, preferably methyl side chains. The contents of monobranched isoparaffins and multi-branched isoparaffins may be given separately. The term "isoparaffin" refers to the total amount of any monobranched isoparaffins and any multi-branched isoparaffins (if present), indicating the total amount of any isoparaffins present regardless of the number of branches. Accordingly, "paraffins" refers to the sum of any normal paraffins, any singly branched isoparaffins, and any multi-branched isoparaffins, if present.

[0029] In the context of the present disclosure, olefin refers to an unsaturated, linear, branched or cyclic hydrocarbon, excluding aromatic compounds. In other words, olefin refers to a hydrocarbon having at least one unsaturated bond, excluding unsaturated bonds in aromatic rings.

[0030] As used herein, cyclic hydrocarbons refer to all hydrocarbons containing a cyclic structure, including cyclic olefins, cycloalkanes, and aromatic hydrocarbons. Cycloalkanes herein refer to cyclic alkanes, i.e., saturated hydrocarbons containing at least one cyclic structure, with or without side chains. Since cycloalkanes are saturated compounds, they are compounds without aromatic ring structures. Aromatic hydrocarbons herein refer to hydrocarbons containing at least one aromatic ring structure, i.e., the ring structure has delocalized alternating π bonds distributed along the ring structure.

[0031] In the context of the present disclosure, for compositions boiling at 36°C or more (at standard atmospheric pressure), the content of n-paraffins, iso-paraffins, mono-branched iso-paraffins, various multi-branched iso-paraffins, cyclo-paraffins and aromatic hydrocarbons is expressed as weight percentage (wt-%) relative to the degassed weight of the feed, stream, effluent, product, component or sample concerned, or, when so defined, as weight percentage (wt-%) relative to the (total) weight of paraffins or the (total) weight of iso-paraffins of the feed, stream, effluent, product, component or sample concerned. The content can be determined by a GCxGC-FID / GCxGC-MS method, preferably carried out as follows: The GCxGC (2D GC) method is operated in accordance with UOP 990-2011 and the experimental part of Nousiainen M. in his master's thesis Comprehensive two-dimensional gas chromatography with massspectrometric and flame ionization detectors in petroleum chemistry, University of Helsinki, August 2017 as generally disclosed, but with the following modifications. The GCxGC was operated in reverse mode using a semipolar column (Rxi17Sil) and then a nonpolar column (Rxi5Sil), followed by an FID detector, using the following operating parameters: carrier gas helium 31.7 cm / sec (column flow 1.60 ml / min at 40 °C); split ratio 1:350; inlet 280 °C; column temperature program 40 °C (0 min)–5 °C / min–250 °C (0 min)–10 °C / min–300 °C (5 min), run time 52 min; modulation period 10 sec; detector 300 °C, H2 40 ml / min, air 400 ml / min; make-up gas helium 30 ml / min; sampling frequency 250 Hz, and injection volume 0.2 μL. Compounds were identified using GCxGC-MS with the following MS parameters: ion source 230 °C; interface 300 °C; scan range 25-500 amu; event time (sec) 0.05; scan speed 20000. Data processing was performed using commercial tools (LabSolutions from Shimadzu and GCImage from Zoex), including identification of detected compounds or hydrocarbon groups and determination of their mass concentrations by applying a response factor relative to n-heptane to the detected peak areas, followed by normalization to 100 wt-%. Unless otherwise reported, olefins were combined with cycloalkanes, and heteroatom species were combined with aromatics. The method had a limit of quantification of 0.1 wt-% for each compound.

[0032] In the context of the present disclosure, various characteristics of a feed, stream, effluent, product, component or sample are determined according to standard methods mentioned or disclosed herein and after appropriate preparation. For example, the cloud point is determined according to ASTM D 5771-17 from a degassed feed, stream, effluent, product, component or sample.

[0033] In the context of the present disclosure, the feed to a reaction stage, in particular the first reaction stage and / or the second reaction stage, is defined such that H2 fed to the respective reaction stage, e.g. H2 fed to hydroisomerization and / or H2 fed to hydrocracking, is excluded from the definition of the feed.

[0034] As used herein, hydroisomerization (HI) effluent refers to total HI effluent, degassed HI effluent, or degassed and stabilized HI effluent, as the case may be, and the term HI effluent may encompass each of these cases.

[0035] In the context of the present disclosure, CX+ paraffin, CX+ normal paraffin, CX+ isoparaffin, CX+ monobranched isoparaffin, CX+ multi-branched isoparaffin, CX+ hydrocarbon or CX+ fatty acid refers to an alkane, normal paraffin, isoparaffin, monobranched isoparaffin, multi-branched isoparaffin, hydrocarbon, or fatty acid having at least X carbon atoms, respectively, wherein X is any feasible integer. It should be understood that not every compound that meets the definition is necessarily present.

[0036] In the context of the present disclosure, CY-alkane, CY-normal alkane, CY-isoalkane, CY-monobranched isoalkane, CY-multi-branched isoalkane, CY-hydrocarbon or CY-fatty acid refers to an alkane, normal alkane, isoalkane, mono-branched isoalkane, multi-branched isoalkane, hydrocarbon or fatty acid having up to Y carbon atoms, respectively, wherein Y is any feasible integer. It should be understood that not every compound that meets the definition must be present.

[0037] In the context of this disclosure, CX Y -CX Z (or CX Y To CX Z ) Alkanes, CX Y -CX Z Normal paraffin, CX Y -CX Z Isoparaffin, CX Y -CX Z Monobranched isoparaffin, CX Y -CX Z Multi-branched isoparaffins, CX Y -CX Z Hydrocarbon or CXY -CX Z Fatty acids refer to a series of paraffins, normal paraffins, isoparaffins, monobranched isoparaffins, multi-branched isoparaffins, hydrocarbons or fatty acids, respectively, where X Y and X Z is a feasible end value integer, wherein the number of carbon atoms within this range is represented by the end value integer and any integer between the end values ​​(if any). However, within the range, especially at or near the end point, all the above-mentioned carbon number paraffins, normal paraffins, isoparaffins, monobranched isoparaffins, multi-branched isoparaffins, hydrocarbons or fatty acids (depending on the specific situation) do not necessarily exist, unless explicitly stated. On the other hand, isomers can include several compounds with the same number of carbon atoms by definition, such as C15 isomers can include methyl tetradecane (different methyl branch positions), dimethyl tridecane (two methyl branch positions are different), etc., wherein "C15 isomer" includes the total amount of all such variants.

[0038] Generally, the total amount by weight or volume of paraffins, normal paraffins, isoparaffins, monobranched isoparaffins, multibranched isoparaffins, hydrocarbons or fatty acids defined each time including all carbon numbers is referred to. For example, C15 to C22 normal paraffins refers to any normal paraffin within the stated range, such as C15, C16, C17, C18, C19, C20, C21 and C22 normal paraffins, even if the content of C15 normal paraffin is zero. In other words, the total amount is obtained by adding 0 (indicating the absence of C15 normal paraffins) to the total weight of all other C15 to C22 normal paraffins present.

[0039] Isomerization converts at least a certain amount of n-paraffins into iso-paraffins, especially mono-branched iso-paraffins. By (further) increasing the degree of isomerization, for example by increasing the severity of the hydroisomerization as described below, more n-paraffins can be converted into iso-paraffins, and mono-branched iso-paraffins can be converted into multi-branched iso-paraffins, such as di-branched and / or triplank iso-paraffins, or even iso-paraffins containing more than three branches.

[0040] As used herein and in the context of the second reaction stage, effective cracking degree refers to cracking that produces non-gaseous (NTP) cracked products, particularly expressed as the ratio of the C8 to C14 hydrocarbon content in the hydrocracked to the C8 to C14 hydrocarbon content in the feed to the second reaction stage.

[0041] As used herein, the term "renewable" refers to compounds or compositions that are obtainable, derivable, or derived from plants and / or animals, including compounds or compositions (in whole or in part) that are obtainable, derivable, or derived from fungi and / or algae. As used herein, renewable compounds or compositions may include genetically manipulated compounds or compositions. Renewable feeds, components, compounds, or compositions may also be referred to as biofeeds, components, compounds, or compositions, or as biogenic feeds, components, compounds, or compositions.

[0042] As used herein, the term "fossil" refers to a compound or composition that is obtainable, derivable or derived from a naturally occurring non-renewable composition, such as crude oil, oil / gas, shale oil / gas, natural gas or coal deposits, etc., and combinations thereof, including any hydrocarbon-rich deposits that can be utilized from above-ground / underground sources. The term "recycled" refers to a recycled material that is generally derived from a non-renewable resource. For example, the term "recycled" may refer to a recycled material derived from discarded plastics.

[0043] The renewable, recycled and fossil compounds or compositions are considered different from each other based on their sources and their impact on environmental issues. Therefore, they may be treated differently under legislative and regulatory frameworks. Usually, renewable, recycled and fossil compounds or compositions are distinguished based on their sources and information provided by the producers.

[0044] Chemically, the renewable or fossil origin of any organic compound, including hydrocarbons, can be determined by suitable methods for analyzing the carbon content of renewable resources, such as DIN 51637 (2014), ASTM D6866 (2020) or EN16640 (2017). The methods are based on the fact that carbon atoms of renewable or biogenic origin contain a greater amount of unstable radiocarbon ( 14 C) atoms. Therefore, by analyzing 12 C and 14The ratio of C isotopes can distinguish carbon compounds derived from renewable or biological sources or raw materials from carbon compounds derived from non-renewable or fossil sources or raw materials. Therefore, a specific ratio of the isotopes can be used as a "marker" to identify renewable carbon compounds and distinguish them from non-renewable carbon compounds. The isotope ratio does not change during the chemical reaction process. Therefore, the isotope ratio can be used to identify renewable compounds, components and compositions and distinguish them from non-renewable fossil materials in reactor feeds, reactor effluents, separated product fractions and various mixtures thereof. Numerically, the biogenic carbon content can be expressed as the amount of biogenic carbon in the material as a weight percentage of the total carbon (TC) in the material (according to ASTM D6866 (2020) or EN 16640 (2017)). In this context, the term "renewable" preferably refers to a material having a biogenic carbon content of greater than 50 wt-%, in particular greater than 60 wt-% or greater than 70 wt-%, preferably greater than 80 wt-%, more preferably greater than 90 wt-% or greater than 95 wt-%, even more preferably about 100 wt-%, based on the total weight of carbon in the material (EN 16640 (2017)).

[0045] According to a first aspect, a hydrocarbon component is provided herein, preferably a renewable diesel fuel component, comprising normal paraffins, monobranched isoparaffins and multi-branched isoparaffins, wherein the total amount of C15-C22 normal paraffins, C15-C22 monobranched isoparaffins and C15-C22 multi-branched isoparaffins is at least 90 wt-% of the total hydrocarbon component weight, or in the range of 90 wt-% to 99 wt-%, and wherein the weight ratio of C15-C22 isoparaffins to C15-C22 normal paraffins is at least 22: 1, preferably at least 24: 1, more preferably at least 30: 1, even more preferably at least 34: 1. High paraffin content gives the hydrocarbon component an excellent cetane number. In addition, compared with traditional hydroprocessed vegetable oils and derived fuel components thereof, high carbon number paraffins ensure higher density. Higher density makes it possible to mix a larger volume of hydrocarbon components into fossil diesel without reducing the density requirements of the blend.

[0046] The inventors have found that the hydrocarbon components of the present invention containing high levels of paraffins in the C15-C22 carbon number range are extremely beneficial for several reasons. For example, high paraffin content makes the space occupied by aromatic hydrocarbons, olefins and cycloalkanes very small, and reducing or minimizing their content helps to meet standards such as EN 15940. High paraffin content may also provide good biodegradability. In addition, the hydrocarbon components of the present invention with high paraffins can provide better performance for end users in terms of combustion and / or emissions. In addition, due to high isoparaffinization, the mixing performance of the hydrocarbon components of the present invention with other typical diesel fuel range components is very good. In addition, compared with components containing higher non-paraffin (especially olefin) content, the high paraffin components of the present invention are more stable or more inert during storage and in blends, because these non-paraffins may react and form high molecular weight precipitates, i.e., colloids, in the component or its blended composition. In addition, aromatic hydrocarbons may be easily unstable, especially when the aromatic hydrocarbon size and concentration increase, resulting in a higher deposition tendency under stress such as caused by aromatic hydrocarbon oxidation and molecular growth. For example, for equipment that is only used seasonally, or using another main power source (such as electricity or gas) and only using diesel as a secondary fuel for a long time in a hybrid vehicle in the fuel system, improved stability is a particularly desirable performance. In addition, a series of paraffins (such as within the C15-C22 range) are more favorable to the final product performance than single or pure components (such as pure C16 paraffins) when blending with other typical diesel fuel range components. Usually, the carbon number distribution of the paraffins in the hydrocarbon component of the present invention covers at least four adjacent carbon numbers in the C15 to C22 range, preferably at least five adjacent carbon numbers, more preferably at least six adjacent carbon numbers. Preferably, hydrocarbon component of the present invention comprises three hydrocarbons with different carbon numbers in the C15-C22 range, and the hydrocarbon content of each carbon number is at least 5 wt-%.

[0047] Therefore, according to certain preferred embodiments, in the hydrocarbon component of the present invention, the total amount of C15-C22 normal paraffins, C15-C22 monobranched isoparaffins and C15-C22 multi-branched isoparaffins is at least 92 wt-%, preferably at least 95 wt-%, and more preferably 95 wt-% to 99 wt-%, based on the weight of the total hydrocarbon component.

[0048] In the hydrocarbon component, the weight ratio of C15-C22 isoparaffins to C15-C22 normal paraffins is at least 22: 1, preferably at least 24: 1, more preferably at least 30: 1, and even more preferably at least 34: 1. The degree of isomerization can set an upper limit for the feasible ratio. The ratio can be from 24: 1 to 1000: 1, preferably from 34: 1 to 1000: 1. Experimental results show that the weight ratio of C15-C22 isoparaffins to C15-C22 normal paraffins has a wide range of high values, typically from about 22: 1 to about 100: 1, such as from about 24: 1 to about 100: 1. When the amount of normal paraffins is close to zero, very high ratios can be achieved. In fact, there will usually be some normal paraffins. The high total amount of paraffins in the C15-C22 range and the very high weight ratio of C15-C22 iso- to C15-C22 normal-paraffins provide a very desirable combination of components: excellent low temperature properties (particularly viscosity at sub-zero temperatures), relatively high density and relatively high viscosity at 40°C, combined with a high cetane number and good low temperature start-up characteristics.

[0049] High C15-C22 paraffin content obviously makes the space that leaves other components to exist very little in the whole hydrocarbon component composition.Therefore, in some preferred embodiments, the total amount of any C1-C14 hydrocarbon is at most 3 wt-% or at most 2 wt-%, or 0.1 wt-% to 3 wt-% of total hydrocarbon component weight.This ensures that hydrocarbon component has higher flash point.The carbon number distribution contributes to the density of hydrocarbon component.In addition, high content of C15-C22 paraffin increases viscosity when above zero temperature.

[0050] Hydrocarbon component of the present invention is highly paraffinized, and most of the paraffins are isomerized.Therefore, in some preferred embodiments, the total amount of all normal paraffins is at most 5 wt-%, preferably at most 3 wt-% of total hydrocarbon component weight. Isoparaffins are associated with good low temperature characteristics relative to the high relative ratio of normal paraffins, and this low temperature characteristics can be further improved by improving the isomerization degree.Dissolved wax also can improve pour point, which may be undesirable, or even disadvantageous in many applications.Very low total content of normal paraffins further reduces the risk of its for example solidification on cold surfaces.

[0051] Preferably, the total amount of C15-C22 isoparaffins in the hydrocarbon component of the present invention is at least 80 wt-%, preferably at least 85 wt-%, more preferably at least 90 wt-%, even more preferably at least 95 wt-%, based on the weight of the total hydrocarbon component. Such embodiments can be regarded as typical.

[0052] A significant proportion of the isoparaffins may contain more than one branch, referred to herein as multi-branched isoparaffins. Preferably, the content or proportion of C15-C22 multi-branched isoparaffins is higher than the mono-branched isoparaffins, the total amount of paraffins or the amount of normal paraffins in the hydrocarbon component, which helps to improve low temperature properties, including fluidity at sub-zero temperatures.

[0053] This can be expressed by the content of C15-C22 mono-branched and multi-branched isoparaffins, in particular by reducing the content of mono-branched isoparaffins and increasing the content of multi-branched isoparaffins. Thus, according to certain embodiments, the hydrocarbon component has a total amount of C15-C22 mono-branched isoparaffins of at most 35 wt-%, preferably at most 30 wt-%, more preferably at most 25 wt-%, based on the weight of the total hydrocarbon component. According to certain other embodiments, the hydrocarbon component has a total amount of C15-C22 multi-branched isoparaffins of at least 60 wt-%, preferably at least 63 wt-%, more preferably at least 65 wt-%, based on the weight of the total hydrocarbon component.

[0054] Another way of expressing this is by the weight ratio of C15-C22 multi-branched isoparaffins to C15-C22 mono-branched isoparaffins, which is at least 1.8, preferably at least 2.0, and more preferably at least 2.5. The ratio can be even higher, such as about 20, as shown in the Examples. According to certain embodiments, the weight ratio of C15-C22 multi-branched isoparaffins to C15-C22 mono-branched isoparaffins can be from 1.8 to 40, such as 2.0 to 25, or 2.0 to 20. Surprisingly, the inventors have found that a high content of multi-branched isoparaffins, or a high ratio of multi-branched isoparaffins / mono-branched isoparaffins, provides excellent low temperature properties for the hydrocarbon component, in particular, its cloud point is much lower than the value expected based only on the weight ratio of C15-C22 isoparaffins to C15-C22 normal paraffins.

[0055] High isoparaffin content, especially high content of multi-branched isoparaffins, enables the incorporation of a higher proportion of heavier paraffins in the C15-C20 range in the hydrocarbon component of the present invention, for example, which helps to increase density, thereby enabling, for example, the hydrocarbon component of the present invention to be incorporated in large quantities into diesel fuel (especially winter or arctic grade diesel fuel) while keeping the density of the diesel fuel within the specification range. Therefore, in certain preferred embodiments, the hydrocarbon component contains at least 35 wt-%, preferably at least 40 wt-%, further preferably at least 45 wt-%, more preferably at least 50 wt-%, even more preferably at least 55 wt-%, most preferably at least 60 wt-%, typically up to 80 wt-% or up to 78 wt-% or up to 76 wt-%, such as 48 wt-% to 80 wt-% or 48 wt-% to 75 wt-% C18 isoparaffins based on the total hydrocarbon component weight. In certain preferred embodiments, the total amount of C19-C22 isoparaffins in the hydrocarbon component is at least 6 wt-% or at least 8 wt-%, preferably at least 9 wt-%, more preferably at least 10 wt-%, typically up to 55 wt-%, or up to 50 wt-%, or up to 45 wt-%, such as up to 40 wt-%, based on the total hydrocarbon component weight. In certain particularly preferred embodiments, the total amount of C19-C22 multi-branched isoparaffins in the hydrocarbon component is at least 5 wt-% or at least 6 wt-%, preferably at least 7 wt-%, more preferably at least 8 wt-%, typically up to 50 wt-%, or up to 45 wt-%, or up to 40 wt-%, such as up to 35 wt-%, based on the total hydrocarbon component weight. Such C19-C22 isoparaffins and / or C19-C22 multi-branched isoparaffin content may be included in the hydrocarbon component having a C18 isoparaffin content as defined above. The C19-C22 isoparaffin, C19-C22 multi-branched isoparaffin and / or C18 isoparaffin content as defined above is particularly advantageously comprised in a hydrocarbon component having a C15-C22 isoparaffin content and / or a ratio of C15-C22 isoparaffin to C15-C22 normal paraffins, and / or a C15-C22 multi-branched isoparaffin content and / or a ratio of C15-C22 multi-branched isoparaffin to C15-C22 mono-branched isoparaffin (as defined above).

[0056] The component of interest here can be defined as a renewable hydrocarbon component, since at least a portion of the raw material from which the component is derived is preferably of non-fossil origin. The biogenic carbon content can be defined for any feasible composition according to EN 16640 (2017). In certain embodiments, the biogenic carbon content of the hydrocarbon component is at least 50 wt-%, preferably at least 70 wt-%, more preferably at least 90 wt-%, or even about 100 wt-%, based on the total weight of carbon (TC) in the hydrocarbon component. Such hydrocarbon components can help increase the biocontent in the product in which they are used. Since hydrocarbon components with biogenic carbon content have extremely low sulfur content, they are also ideal in many uses.

[0057] The kinematic viscosity of the hydrocarbon component at 40°C may be greater than 3.0 mm² / s, preferably greater than 3.9 mm² / s, and more preferably at least 4.0 mm² / s. Based on the experiments carried out, and based on the properties required for various uses, it can be inferred that the upper limit of the kinematic viscosity of the hydrocarbon component at 40°C is less than 7.0 mm² / s, less than 6.0 mm² / s, less than 5.0 mm² / s or less than 4.5 mm² / s. Therefore, in certain preferred embodiments, the kinematic viscosity of the hydrocarbon component at 40°C is greater than 3.0 mm² / s to 7.0 mm² / s, greater than 3.9 mm² / s to 7.0 mm² / s, or greater than 3.9 mm² / s to 6.0 mm² / s, as measured according to EN ISO 3104-2020. The kinematic viscosity of conventional fossil Arctic grade diesel is generally low, such as less than 2.000 mm² / s. The hydrocarbon component of the present invention can be used to improve or optimize the properties of diesel fuel (especially Arctic grade diesel fuel), such as viscosity, cetane number and low temperature properties, or even improve all of the said properties at the same time. For example, the hydrocarbon component of the present invention can be used to increase the viscosity of Arctic grade diesel at 40°C, thereby improving its performance in the fuel system. The higher viscosity improves fuel injection in the fuel system, thereby improving fuel economy. For diesel fuel, the kinematic viscosity preferably meets the EN590:2022 / EN15940:2019 specification limits (maximum viscosity 4.500 mm² / s at 40°C).

[0058] The kinematic viscosity of the hydrocarbon component of the present invention at sub-zero temperatures is lower than the value expected based on its carbon number distribution. This is beneficial when optimizing the properties of blended products (such as diesel fuels), especially when the hydrocarbon component of the present invention is used in Arctic grade diesel blends. Typically, the kinematic viscosity of the hydrocarbon component of the present invention at -20°C can be in the range of 20 mm² / s to 100 mm² / s, preferably 30 mm² / s to 50 mm² / s, more preferably 30 mm² / s to 45 mm² / s, as determined according to EN ISO 3104-2020. When investigating the kinematic viscosity of the hydrocarbon components of the present invention at lower temperatures, it is generally found that the kinematic viscosity of the components at -40°C may be in the range of 160 mm² / s to 200 mm² / s, or 160 mm² / s to 185 mm² / s, and thus can easily meet even stringent sub-zero temperature performance requirements, such as the maximum specification for the kinematic viscosity of low-temperature switchgear oil at -40°C being 400 mm² / s (IEC 60296-2012).

[0059] The higher density of the hydrocarbon component of the present invention is beneficial for providing a higher calorific value compared to conventional hydrotreated vegetable oil derived components. As a result, fuel consumption is slightly lower. Density also affects the blending of components, allowing more hydrocarbon components to be blended into fossil fuels before reaching the lower density specification limit. Typically, the density of the hydrocarbon component at 15°C is at least 780 kg / m³, preferably at least 785 kg / m³, more preferably at least 790 kg / m³, such as in the range of 780 kg / m³ to 800 kg / m³, preferably 785 kg / m³ to 800 kg / m³, more preferably 790 kg / m³ to 795 kg / m³, as determined according to EN ISO 12185-1996.

[0060] In certain embodiments, the flash point of the hydrocarbon component is 100°C or higher, preferably 110°C or higher, more preferably 135°C or higher, such as up to 160°C, for example in the range of 110°C to 150°C, as determined according to ISO 2719-2016 (Pensky-Martens closed cup procedure). Such a flash point is beneficial in certain uses or applications. For example, for low temperature switchgear oils, the flash point should not be less than 100°C.

[0061] The hydrocarbon component was found to have a very low cloud point. In the experiment, the low cloud point value of the hydrocarbon component of the present invention was measured to be lower than -30°C, such as -35°C, -38°C, -41°C, -42°C, -43°C, -44°C, -64°C. Typically, the cloud point of the hydrocarbon component can be -32°C or lower, preferably -35°C or lower, or more preferably -40°C or lower. When expressed as a temperature range, the cloud point of the hydrocarbon component can generally vary in the range of -32°C to -70°C, preferably -35°C to -70°C, such as -40°C to -70°C. The cloud point is preferably determined according to ASTM D 5771-17. For renewable diesel, the cloud point and cold filter plugging point (CFPP) are actually the same. Therefore, the minimum storage temperature (cloud point) of the fuel generally also reflects the minimum operating temperature (CFPP).

[0062] Due to the favorable physicochemical properties, the hydrocarbon component of the present invention is particularly suitable for use as a diesel fuel component, and any characterization or embodiment of the hydrocarbon component of the present invention is applicable to the renewable diesel fuel component described herein. Therefore, according to certain preferred embodiments, the hydrocarbon component of the present invention is a renewable diesel fuel component. Due to the excellent properties at extremely low temperatures (such as -28°C, -34°C, -38°C, and even -44°C), preferably, the hydrocarbon component of the present invention is a renewable Arctic grade diesel fuel component. Examples of Arctic grade diesel are Class 3 and Class 4 diesel according to EN590:2022.

[0063] The cetane number describes the ignition delay of the diesel fuel, and a higher cetane number indicates a shorter ignition delay, which makes it easier to ignite, i.e., the ignition quality of the diesel fuel is better. Typically, the cetane number of the renewable diesel fuel component of the present invention may be at least 51, preferably at least 65, more preferably at least 68, even more preferably at least 70, and most preferably at least 74, as determined according to EN 15195-2014. Typically, the cetane number of the renewable diesel fuel component may be in the range of 51 to 84, such as 68 to 80.

[0064] Higher moisture or water content is also highly undesirable as it can adversely affect, for example, dielectric properties, which is particularly important for transformer oils. Typically, the hydrocarbon component of the present invention may have a water content of at most 100 w-ppm, preferably at most 50 w-ppm, more preferably at most 40 w-ppm, or at most 30 w-ppm, as determined according to IEC 60814.

[0065] The beneficial properties of the hydrocarbon components of the present invention, especially the higher isoparaffin / normal paraffin ratio in the C15-C22 paraffins, can be provided by the production process and its feed. Additives or enhancers to improve low temperature properties or cetane number may not be necessary. The hydrocarbon components can be obtained directly or recovered from the product of the production process.

[0066] In certain embodiments, the hydrocarbon components are obtainable or obtained by a process comprising providing a paraffinic hydrocarbon feed, preferably obtained by hydrodeoxygenation of an oxygenated hydrocarbon feed (typically comprising vegetable oils, animal fats and / or microbial oils), and optionally followed by gas-liquid separation and / or fractionation of the paraffinic feed; and subjecting the paraffinic hydrocarbon feed to at least hydroisomerization, preferably hydroisomerization and hydrocracking, followed by fractionation, and recovering at least the hydrocarbon components from the fractionation. The feeds and process steps, in particular the paraffinic hydrocarbon feed, hydroisomerization and optional hydrocracking and fractionation, are preferably as further defined herein.

[0067] Therefore, according to certain embodiments, the hydrocarbon component of the present invention can be obtained by a process comprising:

[0068] providing a paraffinic hydrocarbon feed comprising at least 60 wt-% paraffins based on the total weight of the paraffinic hydrocarbon feed, wherein at most 30 wt-% of the paraffins are isoparaffins;

[0069] subjecting a paraffinic hydrocarbon feed to hydroisomerization in a first reaction stage, preferably in a first reactor, in the presence of a hydroisomerization catalyst to obtain a hydroisomerization effluent;

[0070] subjecting the second reaction stage feed comprising at least a portion of the hydroisomerization effluent to hydrocracking in a second reaction stage, preferably in a second reactor, in the presence of a hydrocracking catalyst to obtain a hydrocracking effluent;

[0071] The hydrocracking effluent and optionally (at least) a portion of the hydroisomerization effluent are subjected to fractionation and at least hydrocarbon components and optionally aviation fuel components are recovered from the fractionation.

[0072] In addition to the hydrocarbon components and the optionally recovered aviation fuel component, at least a gasoline fuel component and / or a bunker fuel component may be recovered from the fractionation. Optionally, other products may also be recovered.

[0073] Preferably, the process further comprises recovering a recycle stream from the fractionation, the recycle stream preferably having a T5 temperature of 270°C or higher (recovery 5 vol-%, EN ISO 3405-2019) and optionally comprising C16 n-paraffins. The recycle stream may be contained in at least a portion of the hydroisomerization effluent, or constitute at least a portion of the hydroisomerization effluent subjected to hydrocracking in a second reaction zone (preferably a second reactor). In other words, the recycle stream is subjected to hydrocracking in the second reaction stage (preferably in the second reactor) as part of the feed to the second reaction stage. The recycle stream may comprise at least a portion of the fractionation bottoms. In embodiments where the recycle stream is separated, the yield of the desired liquid fuel component may be further optimized, particularly in embodiments where the feed to the second reaction stage of the hydrocracking comprises another portion of the hydroisomerization effluent in addition to the recycle stream. In embodiments where the recycle stream is separated, the hydrocarbon component is preferably recovered by separating a portion from the recycle stream (or in other words, the recycle stream is separated as part of the hydrocarbon component). Thus, the hydrocarbon component may have a T5 temperature of 270°C or higher (recovery 5 vol-%, EN ISO 3405-2019).

[0074] In the process of the present invention, the paraffinic hydrocarbon feed comprises at least 60 wt-%, preferably at least 70 wt-%, more preferably at least 80 wt-%, and even more preferably at least 90 wt-% of the paraffinic hydrocarbon feed gross weight. The paraffinic hydrocarbon feed of the present disclosure may comprise the paraffinic hydrocarbon feed gross weight or even at least 95 wt-% of the paraffinic hydrocarbon feed, or may be substantially composed of paraffinic hydrocarbons. The paraffinic hydrocarbon feed of the present disclosure may contain a small amount of olefins, based on the gross weight of the paraffinic hydrocarbon feed, preferably less than 5 wt-%, more preferably less than 1 wt-%, and a small amount of aromatic hydrocarbons and / or cycloalkanes.

[0075] One advantage of using a high content of paraffinic hydrocarbon feedstock in the process of the present disclosure is that paraffins are relatively easy to isomerize when subjected to hydroisomerization, and can be carried out under milder conditions, compared to, for example, cyclic hydrocarbons. In addition, paraffins are also relatively easy to crack when subjected to hydrocracking, and can be carried out under milder conditions, which helps to reduce the formation of light gases.

[0076] In the process of the present invention, a paraffinic hydrocarbon feed comprising at least 60 wt-% paraffins and at most 30 wt-% of which are isoparaffins, based on the total weight of the paraffinic hydrocarbon feed, can be obtained from a paraffinic hydroprocessing effluent, such as a hydrodeoxygenation (HDO) effluent, a paraffinic Fischer-Tropsch (FT) effluent, or a combination thereof, after subjecting the effluent to at least gas-liquid separation (i.e., removal of compounds that are gaseous at least at NTP), and optionally also to fractionation of the paraffinic feed. Although paraffinic FT effluents of, for example, fossil origin are readily available (in addition to FT effluents of renewable origin), the paraffinic hydrocarbon feed of the present disclosure is at least partially renewable, i.e., comprises biogenic components.

[0077] Preferably, the paraffinic hydrocarbon feed of the present disclosure comprises or consists essentially of a hydrodeoxygenation (HDO) effluent or a fraction thereof from a catalytic hydrodeoxygenation (catalytic HDO) of an oxygenated hydrocarbon feed, such as a degassed hydrodeoxygenation effluent or a fraction thereof. Preferably, the oxygenated hydrocarbon feed comprises at least one or more vegetable oils, animal fats and / or microbial oils. Such paraffinic hydrocarbon feeds tend to have a relatively narrow carbon number distribution compared to FT-based feeds, which typically have a substantially Gaussian distribution of hydrocarbon chains and a broad carbon chain length distribution, and are therefore more able to benefit from the process of the present invention. Typically, providing a paraffinic hydrocarbon feed comprises subjecting the oxygenated hydrocarbon feed to hydrodeoxygenation in the presence of a hydrodeoxygenation catalyst to obtain a hydrodeoxygenation effluent, followed by gas-liquid separation of the hydrodeoxygenation effluent, and optionally fractionating the paraffinic feed to obtain a degassed hydrodeoxygenation effluent or a fraction thereof as a paraffinic hydrocarbon feed. The hydrodeoxygenation can be carried out according to the methods described in prior art publications, such as FI100248B, EP1741768A1, EP2155838B1 or FI129220B1.

[0078] Generally, in the context of the present disclosure, the hydroisomerization (HI) of the paraffinic hydrocarbon feed in the first reaction stage / reactor is operated such that the isomerization reaction predominates while the cracking reactions are controlled or suppressed. Typically, HI in the first reaction stage / reactor is carried out under the following conditions: a temperature in the range of 200°C to 500°C, preferably 230°C to 500°C, more preferably 250°C to 450°C, even more preferably 280°C to 400°C; a pressure in the range of 1 MPa to 10 MPa, preferably 2 MPa to 8 MPa, or 3 MPa to 10 MPa; a H2 partial pressure at the inlet of the first reaction stage / reactor in the range of 1 MPa to 10 MPa, preferably 2 MPa to 8 MPa; a weight hourly space velocity in the range of 0.1 to 10, preferably 0.2 to 8, more preferably 0.4 to 6 kg paraffinic hydrocarbon feed / kg catalyst / hour; and a ratio of H2 to paraffinic hydrocarbon feed in the range of 10 to 2000, preferably 50 to 1000 standard liters of H2 / liter of paraffinic hydrocarbon feed. Hydroisomerization can be carried out according to the methods described in prior art publications, such as FI100248B, EP1741768A1, EP2155838B1 or FI129220 B1. The severity of HI can be increased by one or more of the following methods: reducing WHSV, increasing temperature and / or increasing pressure. When using a new HI catalyst, high severity HI conditions can be achieved at lower temperatures and / or pressures, and / or with higher WHSV, while at the end of the HI catalyst life, higher temperatures and / or pressures, and / or lower WHSVs may be required to achieve moderate severity HI. In the present context, HI producing a liquid effluent having a total isoparaffin content of 50 wt-% to 85 wt-% and a multi-branched isoparaffin content of up to 25 wt-%, or a total isoparaffin content of 85 wt-% to 95 wt-% and a multi-branched isoparaffin content of 25 wt-% to 55 wt-%, or a total isoparaffin content of at least 95 wt-% and a multi-branched isoparaffin content of more than 55 wt-%, based on the wt-% of paraffins in the liquid effluent, is generally regarded as a low severity, or medium severity, or high severity HI, respectively, although these content ranges are intended to illustrate the order of magnitude only and may overlap to some extent and vary from case to case.

[0079] Typically, the hydrocracking operation in the second reaction stage / reactor is such that cracking reactions (particularly those that enhance the effective degree of cracking, especially cracking to C8-C14 hydrocarbons but also cracking to lighter non-gaseous hydrocarbons) are more pronounced than the hydroisomerization in the first reaction stage / reactor. Preferably, in the hydrocracking in the second reaction stage / reactor, cracking reactions (particularly those that enhance the effective degree of cracking) predominate, but generally without excessive cracking and excessive generation of fuel gas. Typically, the hydrocracking in the second reaction section / reactor is carried out under the following conditions: temperature in the range of 200°C to 450°C, preferably 220°C to 430°C, more preferably 280°C to 350°C; pressure in the range of 0.4 MPa to 8 MPa, preferably 1 MPa to 7 MPa; H2 partial pressure at the inlet of the second reaction section / reactor is in the range of 0.4 MPa to 8 MPa, preferably 1 MPa to 7 MPa; weight hourly space velocity in the range of 0.1 to 10, preferably 0.2 to 8, more preferably 0.4 to 6, even more preferably 0.5 to 1.5 kg second reactor feed / kg catalyst / hour; and the ratio of H2 to the second reactor feed is in the range of 10 to 2000, preferably 50 to 1000 standard liters of H2 / liter of second reactor feed.

[0080] Preferably, the hydroisomerization catalyst is a non-sulfided bifunctional hydroisomerization catalyst, and the hydrocracking catalyst is a non-sulfided bifunctional hydrocracking catalyst, preferably the non-sulfided bifunctional catalyst comprises at least one or more metals selected from Group VIII noble metals, more preferably at least one or more metals selected from platinum (Pt) and / or palladium (Pd), and at least one or more acidic porous materials. Non-sulfided bifunctional catalysts are preferred because they do not require sulfidation to maintain their activity during operation, so the sulfur content of various process streams and products can be kept at a low level, and the requirements for H2S separation and recovery are also low. In particular, non-sulfided bifunctional catalysts containing noble metals can be active at lower temperatures than sulfided catalysts and show higher selectivity for isomerization reactions, but are sensitive to deactivation caused by H2S. In particular, for the hydrocracking reaction in the second reaction stage / reactor, bifunctional hydrocracking (HC) catalysts are beneficial because they have at least some isomerization activity in addition to cracking activity and may be particularly effective in effective cracking. As a further advantage, it has been found that bifunctional hydrocracking catalysts comprising at least one or more metals selected from Group VIII noble metals, preferably Pt and / or Pd, show higher activity at relatively low temperatures compared to HC catalysts comprising non-noble metals, thus providing better control of thermal cracking. At low temperatures, the thermodynamic equilibrium tends to shift towards dearomatization, thereby reducing the formation of aromatics by side reactions. Providing the second reaction stage / reactor with a bifunctional HC catalyst also allows the isoparaffin content (wt-% of isoparaffins in the total weight of paraffins) in the hydrocracking effluent to not necessarily be significantly lower than the isoparaffin content in the hydroisomerization effluent, or to be the same or even higher.

[0081] According to certain preferred embodiments, the hydrocarbon component of the present invention can be obtained by a process comprising:

[0082] subjecting an oxygenated hydrocarbon feed comprising at least one or more vegetable oils, animal fats and / or microbial oils to hydrodeoxygenation followed by gas-liquid separation to provide a paraffinic hydrocarbon feed comprising at least 60 wt-% paraffins based on the total weight of the paraffinic hydrocarbon feed, wherein at most 30 wt-% of the paraffins are isoparaffins;

[0083] subjecting a paraffinic hydrocarbon feed to hydroisomerization in a first reaction stage, preferably in a first reactor, in the presence of a hydroisomerization catalyst to obtain a hydroisomerization effluent;

[0084] feeding a second reaction stage comprising at least a portion of the hydroisomerization effluent, optionally comprising a recycle stream, to hydrocracking in the second reaction stage, preferably in a second reactor, in the presence of a hydrocracking catalyst to obtain a hydrocracking effluent;

[0085] The hydrocracking effluent is fractionated and at least the hydrocarbon component and optionally the aviation fuel component is recovered from the fractionation and optionally a recycle stream (as part of the hydrocarbon component) is separated, the recycle stream preferably having a T5 temperature of 270°C or more (recovery 5 vol-%, EN ISO 3405-2019).

[0086] The main component in the paraffinic hydrocarbon feed is normal paraffins. However, the presence of a certain amount of isoparaffins in the paraffinic hydrocarbon feed may still be beneficial. A paraffinic hydrocarbon feed containing a certain amount of isoparaffins can obtain a hydroisomerization effluent having a higher content of multi-branched isoparaffins than an otherwise similar feed that does not contain isoparaffins.

[0087] Preferably, the paraffinic hydrocarbon feedstock of the present disclosure comprises at least 70 wt-%, preferably at least 80 wt-%, more preferably at least 90 wt-% of hydrocarbons having a carbon number in the range of C12 to C30, even more preferably in the range of C14 to C22, of the total weight of the paraffinic hydrocarbon feedstock. These feedstocks can achieve good yields of two or more different types of fuel components and can be easily obtained, for example, from conventional hydrodeoxygenation processes of vegetable oils, animal fats and / or microbial oils (including fatty acids). Paraffinic feedstocks on the heavier side can be obtained from HDO of oils of energy crops (such as Brassica plants), algae oils, crude tall oil (CTO), tall oil fatty acids (TOFA) and / or tall oil pitch (TOP).

[0088] The presence of multi-branched isoparaffins in the hydroisomerization effluent may be considered beneficial because it may have a beneficial effect on the effective degree of cracking in the hydrocracking step. When the desired effective degree of cracking is achieved in the hydrocracking step under milder operating conditions, particularly cracking to C8-C14 hydrocarbons but also cracking to lighter non-gaseous hydrocarbons, overcracking may be avoided and the generation of gaseous hydrocarbons may be reduced. In addition, the increase in the multi-branched isoparaffin content in the hydroisomerization effluent may also be considered beneficial because it may improve the low temperature properties of the hydrocarbon component and the optionally recovered aviation fuel component, and / or improve the RON of the optionally recovered gasoline fuel component. Without being bound by any theory, it is believed that multi-branched isoparaffins are more likely to form two branched paraffin molecules when cracked in the hydrocracking step, rather than one branched paraffin molecule and one normal paraffin molecule, thereby increasing the isoparaffin content in the hydrocracking effluent relative to the normal paraffin content. The same situation is seen downstream of the product recovered by fractionation and the optional recovery of the recycle stream.

[0089] According to certain embodiments, the first reaction section for hydroisomerization and the second reaction section for hydrocracking may be located in the same reactor, for example in separate catalyst beds with their respective equipment. According to certain other embodiments, the first reaction section for hydroisomerization is located in a first reactor, and the second reaction section for hydrocracking is located in a second reactor. Placing the hydroisomerization section in the first reactor and the hydrocracking section in the second reactor has advantages in terms of process design, process control and maintenance.

[0090] Preferably, at least a portion of the hydroisomerization effluent subjected to hydrocracking comprises at least 50 wt-%, further preferably at least 60 wt-%, more preferably at least 70 wt-%, even more preferably at least 80 wt-% of isoparaffins, and optionally at least 5 wt-%, preferably at least 10 wt-%, more preferably at least 15 wt-%, even more preferably at least 20 wt-%, and typically up to 70 wt-% of multi-branched isoparaffins, of the total amount of paraffins in at least a portion of the hydroisomerization effluent. Typically, at least a portion of the hydroisomerization effluent has a cloud point (ASTM D5771-17) of less than 0°C, preferably less than -5°C, more preferably less than -8°C, even more preferably less than -10°C, or less than -15°C.

[0091] Hydrocracking of at least a portion of the hydroisomerization effluent can increase the yield of non-gaseous cracked products, particularly C8-C14 hydrocarbons and lighter non-gaseous hydrocarbons, which contribute to the yield of components in the gasoline and / or aviation fuel range. Since the feed to the hydrocracking may contain a high isoparaffin content and a high multi-branched isoparaffin content, the inventors have found that it is possible to produce further isoparaffins by hydrocracking, rather than reducing their amount, without over-cracking to less valuable light C1-C3 hydrocarbons.

[0092] The advantageous hydrocarbon composition of the hydrocarbon component of the present invention, in particular in connection with a relatively narrow carbon number distribution predominantly in the C15-C22 range, a very high isoparaffin content (and preferably multi-branched isoparaffins) and a very low n-paraffin content, has also been shown to enhance its physicochemical properties, such as those desired for use in diesel fuel compositions, in particular in applications in Arctic diesel fuels. Characteristics that correlate with desired properties of fuels when studied under laboratory conditions are, for example, the shape of the distillation curve and the distillation characteristics.

[0093] According to certain embodiments, there is provided a hydrocarbon component wherein the difference between the T95 temperature (95 vol-% recovery, EN ISO 3405-2019) and the T5 temperature (5 vol-% recovery, EN ISO 3405-2019) is at most 70°C, preferably at most 65°C, more preferably at most 60°C, typically at least 10°C, preferably at least 15°C, more preferably at least 25°C, typically in the range of 10°C to 70°C, preferably 15°C to 70°C, more preferably 20°C to 70°C, even more preferably 25°C to 65°C. While a relatively narrow boiling range may offer certain advantages, a defined minimum boiling range as exemplified herein may also be beneficial, for example for combustion and blending properties. Preferably, the hydrocarbon component has a T5 temperature (recovery 5 vol-%, EN ISO 3405-2019) of 270°C or more, preferably 275°C or more, more preferably 280°C or more, typically between 270°C and 310°C or in the range of 270°C to 310°C, to increase the paraffin content, density and flash point in the C15-C22 range and to allow recovery of aviation fuel components in high yield in the same production process. Typically, the hydrocarbon component may have a final boiling point (FBP) of up to 380°C, preferably up to 370°C, more preferably up to 360°C, even more preferably up to 350°C, as determined according to EN ISO 3405-2019. Such a FBP is generally considered to be in the boiling range of diesel fuel. The hydrocarbon component of the present invention can contain heavier isoparaffins in the C15-C22 range, in particular as defined above, while still being in the diesel boiling range. According to a second aspect, a diesel fuel composition according to the present disclosure comprises a hydrocarbon component or a diesel fuel component as defined previously, preferably a renewable hydrocarbon component or a renewable diesel component, in an amount of 1 vol-% to 99 vol-%, preferably 10 vol-% to 70 vol-%, such as in an amount of at least 10 vol-%, at least 15 vol-%, at least 20 vol-%, at least 25 vol-%, at least 30 vol-%, at least 35 vol-%, at least 40 vol-%, at least 45 vol-%, at least 50 vol-%, at least 55 vol-%, at least 60 vol-%, or at least 65 vol-%, of the total volume of the diesel fuel composition. Surprisingly, a high volume fraction of hydrocarbon components, such as 70 vol-%, is possible in a diesel fuel composition, especially due to the extremely high density compared to conventional paraffinic diesel components.

[0094] The remainder of the diesel fuel composition can be composed of a diesel fuel component and optional additives (especially those common in the prior art). The most common diesel fuel component at present is a fossil diesel grade. For embodiments relating to low temperature storage or operating temperatures, according to EN590:2022, the diesel fuel component (except the present invention's component) can be selected from 0-grade winter diesel grade, 1-grade winter diesel grade, 2-grade winter diesel grade, 3-grade arctic diesel grade or 4-grade arctic diesel grade. Exemplary diesel fuel compositions can comprise hydrocarbon components of the present invention, fossil arctic diesel grade and antioxidants. In certain embodiments, the diesel fuel composition meets the requirement set for diesel fuel in directive 2009 / 30 / EC. In certain embodiments, the requirement of EN590:2022 is also met.

[0095] The blending of the hydrocarbon components of the present invention with arctic grade fossil diesel has been experimentally investigated and reported in the examples in comparison with prior art renewable diesel components. For example, advantages were shown in terms of kinematic viscosity, heating value and low temperature properties of the blends. The results improved as the proportion of the hydrocarbon components of the present invention in the blend increased.

[0096] Thus, according to a third aspect, the hydrocarbon component according to the present disclosure may be used in a diesel fuel composition to improve one or more product properties of the diesel fuel composition. The one or more product properties of the diesel fuel composition include at least one or more of kinematic viscosity at 40°C, cloud point, cold filter plugging point, cetane number, density, heating value and / or biogenic carbon content.

[0097] In certain embodiments, there is provided the use of a hydrocarbon component of the invention for the preparation of a diesel fuel composition that meets the requirements set out in Directive 2009 / 30 / EC for diesel fuels. In certain embodiments, the requirements of EN590:2022 are also met.

[0098] In certain embodiments, the hydrocarbon component can be used in the diesel fuel composition in an amount of 1 vol-% to 99 vol-%, preferably 10 vol-% to 70 vol-%, such as 10 vol-%, 15 vol-%, 20 vol-%, 25 vol-%, 30 vol-%, 35 vol-%, 40 vol-%, 45 vol-%, 50 vol-%, 55 vol-%, 60 vol-% or 65 vol-%, of the total volume of the diesel fuel composition. Such use generally increases the biogenic carbon content of at least the diesel fuel composition.

[0099] Due to its improved properties, the hydrocarbon component of the present invention can be used in a wide range of applications, in particular in arctic grade diesel fuels, where it can be blended in high proportions.

[0100] In addition to use in diesel fuel compositions, the hydrocarbon components of the present invention are suitable for a wide variety of other uses, such as in feedstocks for industrial conversion processes, preferably in thermal cracking feedstocks, such as steam cracking feedstocks and / or catalytic cracking feedstocks; in transformer oils; in heat transfer media or media; in switchgear oils; in shock absorber oils; in insulating oils; in hydraulic fluids; in gear oils; in transmission fluids; in degreasing compositions; in penetrating oils; in corrosion protection compositions; in multipurpose oils; in metalworking fluids; in rolling oils (especially for aluminum); in cutting oils; in drilling fluids; in solvents ; in lubricants; in extender oils; in carriers; in dispersant compositions; in demulsifiers; in extractants; in coating compositions; in coating fluids or pastes; in adhesives; in resins; in varnishes; in printing pastes or inks; in detergents; in cleaning agents; in plasticizing oils; in turbine oils; in hydrophobizing compositions; in agriculture; in crop protection fluids; in construction; in concrete release formulations; in electronics; in medical devices; in compositions for the automotive, electrical, textile, packaging, paper, cosmetic and / or pharmaceutical industries, and / or in the manufacture of intermediates therefor. The increased ratio of isoparaffins to normal paraffins in the hydrocarbon component of the present invention improves fluidity, pumping and mixing characteristics, and blending properties, which are generally desirable and beneficial properties for a wide range of uses, and particularly for uses involving spraying, injection and / or mixing with other ingredients. The use of the hydrocarbon components of the present invention is particularly preferred in transformer oils, but also in thermal and / or catalytic cracking feedstocks for the production of olefin monomers, particularly ethylene and / or propylene, because the very low cyclic compound content helps to reduce the formation of coking aromatics, the very high paraffin content helps to increase the conversion to light olefins even under milder cracking conditions, and the high isoparaffin content is expected to contribute to the formation of favorable propylene to ethylene product ratios in these processes.

[0101] Depending on the intended use, the hydrocarbon component or diesel fuel composition may be suitably added with at least one or more of antioxidants, stabilizers, detergents, corrosion inhibitors, friction modifiers, metal deactivators, lubricity additives, defoamers and / or fuel dyes, for example.

[0102] Process diagram

[0103] Figure 1 A process for producing a hydrocarbon component of the present invention according to an exemplary embodiment is schematically shown. Figure 1In the present invention, an oxygenated hydrocarbon feed 110 is fed to an HDO reactor 120, in which it is hydrodeoxygenated in the presence of an HDO catalyst 130 to obtain a hydrodeoxygenated effluent (HDO effluent) 140, and the obtained HDO effluent 140 is subjected to a gas-liquid separation 150 to separate compounds that are gaseous at least at NTP 160 from the HDO effluent to obtain a degassed HDO effluent 170, which in this exemplary embodiment is a paraffinic hydrocarbon feed as defined herein. The degassed HDO effluent 170 is then separated into a degassed HDO effluent 170 and a degassed HDO effluent 170 is ... Figure 1 The HDO effluent 170 is fed to the first reactor 180, in which the degassed HDO effluent 170 is hydroisomerized in the presence of a hydroisomerization catalyst 190 to obtain a hydroisomerization effluent (HI effluent) 200, and the obtained HI effluent 200 is subjected to a gas-liquid separation 210 to separate compounds that are gaseous at least at NTP 220 from the HI effluent 200 to obtain a degassed HI effluent 230. Figure 1 In the embodiment of the present invention, the degassed HI effluent 230 is fed to a distillation unit 240, which may include a single column or a pre-fractionation and a main distillation column, from which multiple streams or fractions may be obtained. Figure 1 In the distillation, a hydrocarbon component 270 (for example as a diesel fuel component) and an aviation fuel component 260 and / or a gasoline fuel component 250 are recovered. Figure 1 In the fractionation of , the recycle stream 280 having a T5 boiling point of 270°C or higher is also separated, and the hydrocarbon component 270 can be separated as a part thereof. Figure 1 In the second reaction stage feed comprising the recycle stream 280 as at least a portion of the HI effluent is fed to the second reactor 290 where it is hydrocracked in the presence of a hydrocracking catalyst 300 to obtain a hydrocracking effluent 310. Figure 1 In the process, the hydrocracking effluent 310 is subjected to a gas-liquid separation 320, and at least a compound that is gaseous at NTP 330 is separated from the hydrocracking effluent 310 to obtain a degassed hydrocracking effluent 340, and then the degassed hydrocracking effluent 340 is fed to the distillation unit 240 for fractionation together with the degassed HI effluent 230 as a co-feed. In certain embodiments, another portion of the HI effluent 200, 230 may be fed to the second reactor 290 as a co-feed 500 together with the circulating stream 280 (i.e., as a part of the feed to the second reaction stage) for hydrocracking.

[0104] Figure 2 A process for producing a hydrocarbon component of the present invention according to another exemplary embodiment is schematically shown. Figure 2In the present invention, an oxygenated hydrocarbon feed 110 is fed to an HDO reactor 120, in which it is hydrodeoxygenated in the presence of an HDO catalyst 130 to obtain a hydrodeoxygenated effluent (HDO effluent) 140, and the obtained HDO effluent 140 is subjected to a gas-liquid separation 150 to separate compounds that are gaseous at least at NTP 160 from the HDO effluent to obtain a degassed HDO effluent 170, which in this exemplary embodiment is a paraffinic hydrocarbon feed (as defined herein) as defined herein. Then, Figure 2 In the process, the degassed HDO effluent 170 is fed to the first reactor 180, in which the degassed HDO effluent 170 is hydroisomerized in the presence of a hydroisomerization catalyst 190 to obtain a hydroisomerization effluent (HI effluent) 200. The obtained HI effluent 200 is subjected to a gas-liquid separation 210, and compounds that are gaseous at least at NTP 220 are separated from the HI effluent 200 to obtain a degassed HI effluent 230. Figure 2 In the second reaction stage feed including the degassed HI effluent 230 is fed to the second reactor 290, in which it is hydrocracked in the presence of a hydrocracking catalyst 300 to obtain a hydrocracking effluent 350, and the hydrocracking effluent 350 is subjected to a gas-liquid separation 360 to separate compounds that are gaseous at least at NTP 370 from the hydrocracking effluent 350 to obtain a degassed hydrocracking effluent 380. Figure 2 In the embodiment of the present invention, the degassed hydrocracking effluent 380 is fed to the distillation unit 240, which may include a single column or pre-fractionation and main distillation column, where it is fractionated into several streams or fractions. Figure 2 In the distillation of , hydrocarbon component 410 (for example as a diesel fuel component) and aviation fuel component 400 and / or gasoline fuel component 390 are recovered. When separating the recycle stream 420, which preferably has a T5 boiling point of 270° C. or higher, hydrocarbon component 410 can be separated as a part thereof. Figure 2 In the embodiment, the recycle stream 420 can be fed to the second reactor 290 for hydrocracking as a co-feed together with the degassed HI effluent 230 (i.e., as part of the second reaction stage feed). In certain embodiments, a portion of the HI effluent 200, 230 can be fed to the fractionation as a co-feed 500 together with the hydrocracking effluent 350, 380.

[0105] Example

[0106] Example 1 - Production of hydrocarbon components of the invention

[0107] The hydrocarbon components studied herein were recovered from a test run in which four different hydrocracking (HC) feeds (feeds A, B, C and D) were obtained by hydrodeoxygenation (HDO) and gas-liquid separation of two different types of fatty feedstocks, thereby obtaining paraffinic hydrocarbon feeds containing > 95 wt-% of paraffins based on the total weight of the paraffinic hydrocarbon feeds, which were further subjected to hydroisomerization (HI) of different severity. Fractions of the hydroisomerization effluent obtained by degassing the hydroisomerization effluent or by recovering only the bottom fraction were subjected to hydrocracking, followed by degassing or degassing and stabilization of the hydrocracking effluent. A renewable aviation fuel component was recovered from the hydrocracking effluent thus obtained as a main product, and at least a hydrocarbon component was recovered as another product of particular interest herein. The hydrocarbon component thus obtained is a renewable hydrocarbon component. The details of the hydrocracking feed are given in Table 1, and Table 2 shows the process details of the hydrocracking and the approximate boiling point ranges and yields of the hydrocarbon components.

[0108] Table 1. Detailed information of hydrocracking feed

[0109]

[0110] Table 2. Process details of the test run conditions for hydrocracking, cloud point of the degassed hydrocracking effluent, approximate boiling point range of hydrocarbon components (NC) and yield (expressed as wt-% of the degassed HC effluent)

[0111]

[0112] In all test runs, the hydrocracking catalyst was a non-sulfided bifunctional hydrocracking catalyst comprising platinum (Pt) on a zeolite / zeolite-type material. When the feed reported in Table 1 was processed under the hydrocracking conditions reported in Table 2, the catalyst had not only cracking activity but also isomerization activity.

[0113] The hydrocarbon components are recovered in good yields, with yields generally being higher at lower hydrocracking temperatures, higher WHSVs and / or heavier hydrocracking feeds.

[0114] Example 2 - Composition and properties of hydrocarbon components of the present invention

[0115] Some physicochemical and compositional properties of the hydrocarbon components in Example 1 were analyzed and summarized in Tables 3, 4 and 5. The hydrocracking feed HC Feed B and two conventional renewable paraffinic diesels (reference renewable diesel, RRD) obtained by subjecting a fat feedstock to HDO and hydroisomerization and recovering the diesel fraction (i.e., without hydrocracking) were used as references.

[0116] Table 3. Some physicochemical properties of the hydrocarbon components of Example 1

[0117]

[0118] na = not analyzed

[0119] Table 4. Some compositional characteristics of HC feed B, RRD1, RRD2 and hydrocarbon components in Example 1 determined by GCxGC-FID / GCxGC-MS

[0120]

[0121] Table 5. Distillation characteristics of HC feed B and hydrocarbon components in Example 1 (according to EN ISO 3405-2019)

[0122]

[0123] Some variations can be seen due to process conditions, target cut start point, and / or use of different HC feeds in the test runs. However, based on Table 3 it can be concluded that the cloud point (and CFPP) temperature varies from -35°C to -64°C, the kinematic viscosity at 40°C varies from 3.668 mm² / s to 4.368 mm² / s, the cetane number is > 68, and the density of the components is high with only slight variations (787 kg / m³-793 kg / m³).

[0124] As can be seen from Table 4, the hydrocarbon component in Example 1 mainly comprises C15-C22 paraffins, which have isoparaffins as the main part (> 96 wt-%). In terms of carbon number, the main isoparaffins are C18 isoparaffins, more specifically C18 isoparaffins with two or more branches (data not reported here). Depending on the process conditions, about 48 wt-% to about 75 wt-% of all paraffins are C18 isoparaffins. The weight ratio of C15-C22 isoparaffins to C15-C22 normal paraffins of the hydrocarbon component in Example 1 is >22, i.e. much higher than that in HC feed B used as a reference here. In addition, the hydrocarbon component in Example 1 has a lower total normal paraffin content, a lower monobranched isoparaffin content (< 30 wt-%), and a higher multi-branched isoparaffin content (> 65 wt-%) compared to HC feed B and RRD.

[0125] Example 3 - Comparison of the physicochemical properties of the hydrocarbon component (NC), hydrocracking feed and paraffinic reference renewable diesel (RRD) of the present invention

[0126] The following comparison shows that the hydrocarbon component (NC) of the present invention is significantly different from the hydrocracking feed (HC feed B) and two conventional paraffinic renewable diesels (reference renewable diesel, RRD, the same as in the previous example). Table 6 shows some physicochemical characteristics of HC feed B, RRD 1 and RRD 2, and two hydrocarbon components (NC_TR3, NC_TR8) obtained from test runs 3 and 8, the average characteristics (average NC) of five hydrocarbon components obtained from five different test runs (TR) of hydrocracking HC feed B according to the present disclosure at different HC conditions, and the average characteristics (average NC) of three components obtained from three different test runs (TR) of hydrocracking HC feed C under different HC conditions according to the present disclosure.

[0127] Table 6. Average properties of HC feed B, RRD1 and RRD2, hydrocarbon components NC_TR3 and NC_TR8, and hydrocarbon components obtained from 5 and 3 different TRs (average NC)

[0128]

[0129] * EN ISO 3104-2020; ** ISO 2719-2016 (Pensky-Martin closed cup method)

[0130] The results in Table 6 show that hydrocarbon components with excellent low cloud points, improved kinematic viscosity at 40°C, and high density can be obtained from different HC feeds under different test operating conditions. The individual cloud points and average cloud points of the new components are at least about 10°C lower than the cloud points of the hydrocracking feed and RRD. The individual kinematic viscosity and average kinematic viscosity of the hydrocarbon component of the present invention at 40°C are significantly higher than the kinematic viscosity of RRD, and are also significantly higher than the viscosity of the hydrocracking feed. The cetane number of the new component is roughly at the same level as the cetane number of the hydrocracking feed and RRD, and significantly exceeds the cetane number requirement of at least 51.0 for Class B paraffinic diesel, and even exceeds the cetane number requirement of at least 70.0 for Class A paraffinic diesel (EN 15940-2016). The individual density and average density of the hydrocarbon component of the present invention are significantly higher than the density of RRD, and are also significantly higher than the density of HC feed B.

[0131] Example 4 - Blending Experiments with Arctic Grade Fossil Diesel

[0132] The physicochemical properties in Example 3 have shown that the hydrocarbon component of the present invention is an excellent blending component, especially for diesel fuel compositions. In these blending examples, the suitability of the hydrocarbon component of the present invention as an arctic / severe winter diesel grade is demonstrated. As reference components, conventional paraffinic renewable diesel (reference renewable diesel, RRD) and conventional fossil arctic grade diesel were used. These blending examples were linearly calculated using the properties of the pure blending components (NC_TR8, RRD and fossil arctic grade).

[0133] Table 7. Blending test results

[0134]

[0135] * Assuming the calorific value of NC and RRD is 44.0 MJ / kg.

[0136] **Percentages are expressed as vol-% of the total volume of the blend.

[0137] For example, when 10 vol-% NC_TR8 is blended with fossil Arctic grade diesel, a viscosity of nearly 2 mm² / s is achieved (at 40°C). This viscosity is significantly higher than the viscosity achieved when 10 vol-% RRD is blended with fossil Arctic grade diesel.

[0138] Furthermore, the viscosity advantage is more pronounced when 25 vol-% NC_TR8 is included in the blend compared to when RRD is used as a blending component. In addition, the cloud point of arctic grade diesel is not increased when NC_TR8 is used as a blending component, whereas the opposite is true when RRD is used as a blending component, which may actually reduce the cloud point of arctic grade diesel due to the very low cloud point of NC-TR8.

[0139] According to the diesel fuel specification for climate-related requirements for use in arctic or severe winter climates (EN590:2022 Table 3), a Class 4 diesel fuel should have a cloud point of maximum -34°C, a density at 15°C in the range of 800 kg / m³ to 840 kg / m³, a kinematic viscosity at 40°C in the range of 1.200 to 4.000, a cetane number of minimum 51.0 within the EU, and, in terms of distillation characteristics, a maximum recovery of 10.0 vol-% at 180°C and a minimum recovery of 95.0 vol-% at 340°C. Although the density of the inventive hydrocarbon component (NC) tested here is slightly below 800 kg / m³, the other mentioned characteristics are fully in compliance with the Class 4 diesel fuel specification requirements and thus allow the incorporation of the inventive hydrocarbon component into arctic / winter diesel fuel compositions in proportions much greater than, for example, the paraffinic reference renewable diesel (RRD) tested herein.

[0140] Furthermore, the examples show that using NC as a blending component instead of RRD allows the blend to achieve a higher calorific value per litre. This is a major advantage as it leads directly to lower fuel consumption.

[0141] Various embodiments have been presented. It should be understood that in this document, the words "comprise", "include" and "contain" are each used as open-ended expressions, and no exclusivity is intended. The above description has provided a complete and informative description of the best mode currently contemplated by the inventors for implementing the present invention by way of non-limiting examples of specific implementations and embodiments. However, it is clear to those skilled in the art that the present invention is not limited to the details of the embodiments presented above, but can be implemented in other embodiments using equivalent means or different combinations of embodiments without departing from the features of the present invention.

[0142] In addition, some features of the exemplary embodiments disclosed above may be used advantageously without the corresponding use of other features. Therefore, the above description should be regarded as merely an illustration of the principles of the present invention and not limited thereto. Therefore, the scope of the present invention is limited only by the attached patent claims.

Claims

1. A hydrocarbon component comprising a normal chain alkane, a single-branch isoalkane and a multi-branch isoalkane, wherein: The total amount of C15-C22 n-alkali, C15-C22 single-branch isoparaffin and C15-C22 multi-branch isoparaffin is at least 90 wt-% of the total hydrocarbon component weight, and wherein The weight ratio of C15-C22 isoalkane to C15-C22 n-alkane is at least 22:1, preferably at least 24:1, more preferably at least 30:1, even more preferably at least 34:

1.

2. The hydrocarbon component of claim 1, wherein the total amount of C1-C14 hydrocarbons is at most 3 wt-% by weight of the total hydrocarbon component.

3. The hydrocarbon component of claim 1 or 2, wherein the total amount of the total n-alkanes is at most 5 wt-%, preferably at most 3 wt-%, of the weight of the total hydrocarbon component.

4. The hydrocarbon component according to any of the preceding claims, wherein the weight ratio of C15-C22 multi-branch isoparaffin to C15-C22 single-branch isoparaffin is at least 1.8, preferably at least 2.0, more preferably at least 2.

5.

5. The hydrocarbon component according to any one of the preceding claims, wherein the total amount of C15-C22 isoparaffins is at least 80 wt-%, preferably at least 85 wt-%, more preferably at least 90 wt-%, even more preferably at least 95 wt-%, based on the weight of the total hydrocarbon component.

6. The hydrocarbon component according to any one of the preceding claims, wherein the total amount of C15-C22 multi-branched isoparaffins is at least 60 wt-%, preferably at least 63 wt-%, more preferably at least 65 wt-%, based on the weight of the total hydrocarbon component, and / or the total amount of C15-C22 mono-branched isoparaffins is at most 35 wt-%, preferably at most 30 wt-%, more preferably at most 25 wt-%, based on the weight of the total hydrocarbon component.

7. The hydrocarbon component according to any one of the preceding claims, wherein the total amount of C15-C22 normal paraffins, C15-C22 monobranched isoparaffins and C15-C22 multibranched isoparaffins is at least 92 wt-%, preferably at least 95 wt-%, more preferably 95 wt-% to 99 wt-%, based on the weight of the total hydrocarbon component.

8. A hydrocarbon component according to any one of the preceding claims, having a difference between a T95 temperature (95 vol-% recovery, EN ISO 3405-2019) and a T5 temperature (5 vol-% recovery, EN ISO 3405-2019) of at most 70°C, preferably at most 65°C, more preferably at most 60°C, and / or at least 10°C, preferably at least 15°C, more preferably at least 25°C, and / or in the range of 10 to 70°C, preferably 15 to 70°C, more preferably 20 to 70°C, even more preferably 25 to 65°C.

9. The hydrocarbon component according to any of the preceding claims, wherein the kinematic viscosity of the hydrocarbon component at 40°C is greater than 3.0 mm² / s, preferably greater than 3.9 mm² / s, more preferably at least 4.0 mm² / s, determined according to EN ISO 3104-2020; and / or wherein the kinematic viscosity of the hydrocarbon component at -20°C is in the range of 20 mm² / s to 100 mm² / s, preferably 30 mm² / s to 50 mm² / s, more preferably 30 mm² / s to 45 mm² / s, determined according to EN ISO 3104-2020.

10. The hydrocarbon component according to any one of the preceding claims, wherein the hydrocarbon component has a flash point of 100°C or higher, preferably 110°C or higher, more preferably 135°C or higher, as determined according to ISO 2719-2016 (Pensky-Martin closed cup method).

11. The hydrocarbon component according to any one of the preceding claims, wherein the hydrocarbon component has a density at 15°C of at least 780 kg / m³, preferably at least 785 kg / m³, more preferably at least 790 kg / m³, determined according to EN ISO 12185-1996.

12. The hydrocarbon component according to any of the preceding claims, wherein the cloud point of the hydrocarbon component is -32°C or less, preferably -35°C or less, more preferably -40°C or less, according to ASTM D 5771-17.

13. The hydrocarbon component according to any one of the preceding claims, wherein the hydrocarbon component has a biogenic carbon content of at least 50 wt-%, preferably at least 70 wt-%, more preferably at least 90 wt-%, or even more preferably about 100 wt-%, based on the total weight of carbon (TC) in the hydrocarbon component, determined according to EN 16640 (2017).

14. The hydrocarbon component according to any of the preceding claims, which can be obtained or obtained by a process including: providing a paraffinic hydrocarbon feed, preferably obtained by hydrodeoxygenating an oxygenated hydrocarbon feed, typically comprising vegetable oils, animal fats and / or microbial oils, and optionally subsequent gas-liquid separation and / or fractionation of the paraffinic feed, and The paraffin-based hydrocarbon feed is subjected to at least hydroisomerization, preferably hydroisomerization and hydrocracking, followed by fractionation and at least the hydrocarbon component is recovered from the fractionation.

15. The hydrocarbon component according to any of the preceding claims, which can be obtained by a method including: A paraffin-based hydrocarbon feed is provided, the paraffin-based hydrocarbon feed comprising at least 60 wt-% of the paraffin-based hydrocarbon feed, wherein up to 30 wt-% of the paraffin-based hydrocarbon feed is isoparaffin; The paraffin-based hydrocarbon feed is subjected to hydroisomerization in the first reaction stage, preferably in the first reactor, in the presence of a hydroisomerization catalyst to obtain a hydroisomerization effluent; subjecting a second reaction stage feed comprising at least a portion of said hydroisomerization effluent to hydrocracking in a second reaction stage, preferably in a second reactor, in the presence of a hydrocracking catalyst to obtain a hydrocracking effluent; The hydrocracked effluent and optionally a portion of the hydroisomerized effluent are fractionated and at least the hydrocarbon component and optionally the aviation fuel component are recovered from the fractionation.

16. The hydrocarbon component according to any of the preceding claims, wherein the hydrocarbon component is a diesel fuel component, preferably an Arctic grade diesel fuel component.

17. The hydrocarbon component according to claim 16, wherein the hydrocarbon component has a cetane number of at least 51, preferably at least 65, more preferably at least 68, even more preferably at least 70, most preferably at least 74, determined according to EN 15195-2014.

18. A diesel fuel composition comprising 1 vol-% to 99 vol-%, preferably 10 vol-% to 70 vol-% of the total diesel fuel composition volume of the hydrocarbon component according to any one of claims 1 to 17.

19. Use of the hydrocarbon component according to any one of claims 1 to 17 in a diesel fuel composition for improving one or more product properties of the diesel fuel composition, the one or more product properties of the diesel fuel composition preferably comprising at least one or more of kinematic viscosity at 40°C, cloud point, cold filter plugging point, cetane number, density, calorific value and / or biogenic carbon content.

20. Use according to claim 19 or a diesel fuel composition according to claim 18, wherein the diesel fuel composition meets the diesel fuel requirements set out in Directive 2009 / 30 / EC and optionally in EN590:2022.

21. Use according to claim 19 or 20, wherein the diesel fuel composition comprises the hydrocarbon component according to any one of claims 1 to 17 in an amount of 1 to 99 vol-%, preferably 10 to 70 vol-% by volume of the total diesel fuel composition.

22. The hydrocarbon component according to any one of claims 1 to 17 in a feedstock for an industrial conversion process, preferably a thermal cracking feedstock and / or a catalytic cracking feedstock; in a transformer oil; in a heat transfer medium or media; in a switchgear oil; in a shock absorber oil; in an insulating oil; in a hydraulic fluid; in a gear oil; in a transmission fluid; in a degreasing composition; in a penetrating oil; in an anti-corrosion composition; in a multi-purpose oil; in a metalworking fluid; in a rolling oil, in particular in a rolling oil for aluminum; in a cutting oil; in a drilling fluid; in a solvent; in a lubricant; in an extension oil; in carriers; in dispersant compositions; in demulsifiers; in extractants; in coating compositions; in coating fluids or pastes; in adhesives; in resins; in varnishes; in printing pastes or inks; in detergents; in cleaning agents; in plasticizing oils; in turbine oils; in hydrophobizing compositions; in agriculture; in crop protection liquids; in construction; in concrete release formulations; in electronics; in medical devices; in compositions for the automotive, electrical, textile, packaging, paper, cosmetic and / or pharmaceutical industries, and / or in the manufacture of intermediates therefor.

23. The use according to any one of claims 19 to 22, or the diesel fuel composition according to claim 18 or 20, or the hydrocarbon component according to any one of claims 1 to 17, wherein the hydrocarbon component or the diesel fuel composition has added thereto at least one or more of an antioxidant, a stabilizer, a detergent, a corrosion inhibitor, a friction modifier, a metal deactivator, a lubricity additive, a defoamer and / or a fuel dye.

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