Gasoline fuel component

Abstract

This specification discloses a gasoline fuel component mainly containing C4 - C9 n - paraffins, C4 - C9 mono - branched i - paraffins, and C4 - C9 multi - branched i - paraffins. In the gasoline fuel component, the weight ratio of at least certain i - paraffins to certain n - paraffins is higher than that in gasoline components of the prior art. This gasoline fuel component can provide improved blendability, octane number, and combustion characteristics.

Description

Technical Field

[0001] The present disclosure generally relates to gasoline fuels, and more specifically to gasoline fuels containing blends of gasoline components. The present disclosure relates in particular, but not exclusively, to novel gasoline fuel components that can be obtained from renewable feedstocks.

Background Art

[0002] This section presents useful background technical information without admitting that any of the techniques described herein represent the state of the art.

[0003] There continues to be a need to reduce greenhouse gas emissions and / or carbon footprint in transportation. Accordingly, there is increasing interest in renewable transportation fuels.

[0004] Processes have been proposed for producing gasoline fuel components from renewable feedstocks. However, the octane number of such gasoline fuel components has been relatively low (compared to other conventional gasoline fuel components). There is a need to improve the quality of renewable gasoline fuel components. In particular, there is interest in producing renewable gasoline fuel components that can be used in large quantities together with additional gasoline components in gasoline fuel compositions.

Summary of the Invention

Problems to be Solved by the Invention

[0005] It is an object to solve or mitigate at least some of the problems associated with the prior art. The object is to improve the quality of gasoline fuel components that can be obtained from renewable sources.

Means for Solving the Problems

[0006] The appended claims define the scope of protection. Any examples and technical explanations of products, processes, and / or uses in the description and / or drawings that are not covered by the claims are presented as useful examples for understanding the invention, rather than as embodiments of the invention.

[0007] According to a first exemplary embodiment, a gasoline fuel component comprising n-paraffins, mono-branched i-paraffins, and multi-branched i-paraffins, wherein the total amount of C4-C9 n-paraffins, C4-C9 mono-branched i-paraffins, and C4-C9 multi-branched i-paraffins is more than 90 wt-% of the total weight of the gasoline fuel component, and the weight ratio of C8 i-paraffins to C8 n-paraffins is at least 4.0, preferably at least 4.5, more preferably at least 5.0, even more preferably at least 5.5, still more preferably at least 6.0, and optionally, the total amount of C8 n-paraffins and C8 i-paraffins is at least 1.0 wt-%, preferably at least 2.5 wt-%, more preferably at least 5.0 wt-%, even more preferably at least 5.5 wt-%, still more preferably at least 6.0 wt-%, most preferably at least 7.0 wt-% of the total weight of the gasoline fuel component, a gasoline fuel component is provided.

[0008] The inventors have found that the gasoline fuel component and its embodiments provide advantages compared to prior art gasoline components. The advantages are related to, for example, better blendability, higher octane number, and better combustion characteristics, which will be described in more detail later.

[0009] The production of the gasoline fuel component can use a specific process including a combination of hydroisomerization and hydrocracking of a paraffinic feedstock. The gasoline fuel component can be obtained from a process for producing renewable fuel components, and the process further includes the recovery of aviation fuel components.

[0010] According to a second exemplary embodiment, the use of the present gasoline fuel component in a gasoline fuel composition is provided.

[0011] According to a third exemplary embodiment, a gasoline fuel composition comprising the present gasoline fuel component is provided. The above use and gasoline fuel composition provide a commercial liquid transportation fuel product, wherein the present gasoline fuel component can contribute to the bio-content and can provide better blendability, combustion characteristics and a higher octane number.

[0012] According to a fourth exemplary embodiment, in raw materials for industrial conversion processes, preferably in pyrolysis raw materials and / or catalytic cracking raw materials, in solvents, carriers, dispersant compositions, demulsifiers, extractants, surfactants, degreasing compositions, detergents, thinners, penetration oils, anticorrosion compositions, multi-purpose oils, in metal processing, in agriculture, in construction, in electronic devices, in medical devices, in compositions for the automotive, electrical, textile, packaging, paper and / or pharmaceutical industries, and / or in the manufacture of intermediates therefor, the use of the present gasoline fuel component is provided.

[0013] Exemplary embodiments and implementations without various constraints are shown above. The foregoing embodiments are used only to illustrate selected embodiments or steps that can be utilized in different implementations. Some embodiments may be presented only with reference to specific exemplary embodiments. It should be understood that the corresponding embodiments can also be applied to other exemplary embodiments.

Brief Description of the Drawings

[0014] Some exemplary embodiments are described with reference to the accompanying drawings.

[0015]

Figure 1

Figure 2

Best Mode for Carrying Out the Invention

[0016] In the following description, like reference numerals denote like elements or steps.

[0017] All standards referred to in this specification are the latest revised versions available at the filing date, unless otherwise specified.

[0018] Unless otherwise specified, for distillation characteristics such as initial boiling point (IBP), final boiling point (FBP), T5 temperature (5 vol-% recovery), T10 temperature (10 vol-% recovery), T95 temperature (95 vol-% recovery), and boiling point range, EN ISO3405-2019 is referred to. The IBP is the temperature at the moment when the first droplet of condensate falls from the lower end of the condenser tube, and the FBP is the maximum thermometer measurement value obtained during the test, which usually occurs after all the liquid has evaporated from the bottom of the flask. For boiling point distribution, a GC-based method (simdis) ASTM D2887-19e1, or for hydrocarbons in the gasoline range, ASTM D7096-19 can also be referred to.

[0019] As used in the context of the present disclosure, "gasoline fuel component" is the subject of the present invention and is mainly formed from paraffinic hydrocarbons, as defined in more detail later. This can preferably be obtained as a cut or fraction from one or more processes that purify the feedstock in several steps and fractionate the product into cuts. Typically, such a gasoline fuel component, as determined according to EN ISO3405-2019, boils within the range of about 25 °C to about 210 °C, i.e., has an IBP and an FBP. This means providing a component that can be used at least together with at least one other gasoline component to form a "gasoline fuel composition". The above gasoline fuel composition can be commercially sold as gasoline, gasoline fuel, petrol, and refers to a product that can be used as fuel for a spark-ignition engine. The above gasoline fuel composition meets one or more standard specifications of gasoline fuel, such as the specifications defined in EN 228-2012+A1-2017. Typically, a gasoline fuel composition is a blend of two or more gasoline fuel components.

[0020] As used in the context of the present disclosure, "aviation fuel component" refers to a hydrocarbon composition suitable for use in a fuel composition that meets the standard specifications of aviation fuel, such as the specifications defined in ASTM D7566-21. Typically, such an aviation fuel component, as determined according to EN ISO3405-2019, boils within the range of about 100 °C to about 300 °C, for example within the range of about 150 °C to about 300 °C, i.e., has an IBP and an FBP.

[0021] As used in the context of the present disclosure, "diesel fuel component" refers to a hydrocarbon composition suitable for use in a fuel composition that meets the standard specifications of diesel fuel, such as the specifications defined in EN 15940:2016+A1:2018+AC:2019 or EN 590:2022. Typically, such a diesel fuel component, as determined according to EN ISO3405-2019, boils within the range of about 160 °C to about 380 °C, i.e., has an IBP and an FBP.

[0022] As used herein, hydrocarbon refers to a compound consisting of carbon and hydrogen. Hydrocarbons of particular interest in this context include paraffins, n - paraffins, i - paraffins, mono - branched i - paraffins, multi - branched i - paraffins, olefins, naphthenes, and aromatics. Oxygen - containing hydrocarbons refer to hydrocarbons containing covalently - bonded oxygen herein.

[0023] As used herein, paraffin refers to an acyclic alkane, i.e., an acyclic open - chain saturated hydrocarbon that is either straight - chain (normal paraffin, n - paraffin) or branched (isoparaffin, i - paraffin). In other words, paraffin refers to n - paraffin and / or i - paraffin herein.

[0024] In the context of the present disclosure, i - paraffin refers to a branched open - chain alkane, i.e., an acyclic open - chain saturated hydrocarbon having one or more alkyl side - chains. As used herein, an i - paraffin having one alkyl side - chain or branch is called a mono - branched i - paraffin, and an i - paraffin having two or more alkyl side - chains or branches is called a multi - branched i - paraffin herein. In other words, i - paraffin refers to mono - branched i - paraffin and / or multi - branched i - paraffin herein. The alkyl side - chains of i - paraffins may be, for example, C1 - C6 alkyl side - chains, preferably methyl side - chains. The amounts of mono - branched and multi - branched i - paraffins may be given separately. The term "i - paraffin" refers to the total amount of any mono - branched i - paraffin and any multi - branched i - paraffin present, and indicates the total amount of any i - paraffin present regardless of the number of branches. Correspondingly, "paraffin" refers to the total amount of any n - paraffin, any mono - branched i - paraffin, and multi - branched i - paraffin present.

[0025] In the context of the present disclosure, olefin refers to an unsaturated, straight - chain, 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.

[0026] As used herein, cyclic hydrocarbons refer to all hydrocarbons containing a cyclic structure, including cyclic olefins, naphthenes, and aromatics. Naphthenes, as used herein, refer to cycloalkanes, i.e., saturated hydrocarbons containing at least one cyclic structure, with or without side chains. Since naphthenes are saturated compounds, they are compounds without an aromatic ring structure. Aromatics, as used herein, refer to hydrocarbons containing at least one aromatic ring structure, i.e., a cyclic structure having alternating π-bonds delocalized throughout the circumference of the above cyclic structure.

[0027] In the context of the present disclosure, for a composition that boils at <250 °C (at standard atmospheric pressure), the contents of n-paraffin, i-paraffin, mono-branched i-paraffin, various multi-branched i-paraffins, olefins, naphthenes and aromatics are expressed as weight % (wt-%) relative to the weight of the feed, stream, effluent, product, component or sample, or, if so defined, as weight % (wt-%) relative to the (total) weight of the paraffins or the (total) weight of the i-paraffins of the feed, stream, effluent, product, component or sample. The above contents can be determined by the GC-FID / GC-MS method, preferably carried out as follows: The GC-FID disclosed in ASTM D6839 was used with the parameters: column ZB-1 60 m, ID 0.25 mm, df 1.0 micron, or similar; oven 0 °C (2 min) - 1.5 °C / min 300 °C (5 min); injector and detector 300 °C; carrier gas helium 1.0 ml / min; detector gas H2 35 ml / min and air 350 ml / min; make-up flow helium 30 ml / min; split flow 165:1 (165 ml / min). Individual compounds were identified using GC-MS (run parameters: ion source 230 °C; interface 280 °C; scan 25 - 280 m / z; scan rate 303; scan event time 0.88). Commercial tools (LabSolutions / GCMSSolutions from Shimadzu and OpenLab from Agilent) were used to identify the detected compounds or hydrocarbon groups and to determine their mass concentrations by applying the response factor to n-heptane to the area of the detected peak and subsequently normalizing to 100 wt-% (in the case of liquid volume concentration: by applying the density factor to the calculated mass concentration of the detected peak and subsequently normalizing to 100 vol-%). Cyclic olefins are grouped together with naphthenes. The quantification limit of individual compounds for this method is 0.1 wt-%.

[0028] In the context of the present disclosure, for hydrocracked feeds and other compositions of similar boiling ranges, the contents of n-paraffins, i-paraffins, mono-branched i-paraffins, various multi-branched i-paraffins, naphthenes and aromatics are expressed as weight % (wt-%) relative to the degassed weight of the feed, stream, effluent, product, component or sample, or, if so defined, as weight % (wt-%) relative to the (total) weight of paraffins or the (total) weight of i-paraffins of the feed, stream, effluent, product, component or sample. The above contents can be determined by the GC×GC-FID / GC×GC-MS method, preferably as follows: The GC×GC (2D GC) method was carried out with the following modifications as generally disclosed in UOP990-2011 and by Nousiainen M. in the experimental section of his master's thesis Comprehensive two-dimensional gas chromatography with mass spectrometric and flame ionization detectors in petroleum chemistry (University of Helsinki, August 2017): GC×GC was first carried out using a semi-polar column (Rxi17Sil), followed by a non-polar column (Rxi5Sil), and subsequently using an FID detector with the following operating parameters: carrier gas helium 31.7 cm / sec (column flow rate at 40 °C 1.60 ml / min); split ratio 1:350; injector 280 °C; column T 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 with H2 40 ml / min and air 400 ml / min; makeup flow helium 30 ml / min; sampling rate 250 Hz and injection size 0.2 microliters, and was run in reverse mode. GC×GC-MS was used to identify individual compounds 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.Commercially available tools (Shimadzu's LabSolutions, Zoex's GC images) were used for data processing including the identification of detected compounds or hydrocarbon groups, and for determining their mass concentrations by applying the response factor for n-heptane to the volume of the detected peaks and subsequently normalizing to 100 wt-%. Olefins were grouped with heteroatomic species having naphthenes and aromatics unless otherwise reported. The quantification limit for individual compounds by this method is 0.1 wt-%.

[0029] In the context of the present disclosure, various properties of feeds, streams, effluents, products, components or samples are determined according to standard methods appropriately prepared and referenced or disclosed herein. For example, cloud point is determined from a degassed feed, stream, effluent, product, component or sample according to ASTM D5771-17.

[0030] In the context of the present disclosure, feeds to the reaction section, particularly the first reaction section and / or the second reaction section, are defined such that H2 that may be fed to each reaction section, such as H2 fed to hydroisomerization and / or H2 fed to hydrocracking, is excluded from the definition of the feed.

[0031] As used herein, the hydroisomerization (HI) effluent may in some cases refer to the total HI effluent, the degassed HI effluent, or the degassed and stabilized HI effluent, and the term HI effluent may encompass each of these.

[0032] In the context of the present disclosure, CX+ paraffin, CX+ n-paraffin, CX+ i-paraffin, CX+ mono-branched i-paraffin, CX+ multi-branched i-paraffin, CX+ hydrocarbon, or CX+ fatty acid each refer to a paraffin, n-paraffin, i-paraffin, mono-branched i-paraffin, multi-branched i-paraffin, hydrocarbon, or fatty acid having at least X carbon atoms, where X is any achievable integer. It is understood that not all compounds falling within the definition necessarily exist.

[0033] In the context of the present disclosure, CY-paraffin, CY-n-paraffin, CY-i-paraffin, CY-monobranched i-paraffin, CY-multibranched i-paraffin, CY-hydrocarbon, or CY-fatty acid each refers to a paraffin, n-paraffin, i-paraffin, monobranched i-paraffin, multibranched i-paraffin, hydrocarbon, or fatty acid having a maximum of Y carbon atoms, where Y is any achievable integer. In the context of the present disclosure, CX Y -CX Z (or CX Y -CX Z ) paraffin, CX Y -CX Z n-paraffin, CX Y -CX Z i-paraffin, CX Y -CX Z monobranched i-paraffin, CX Y -CX Z multibranched i-paraffin, CX Y -CX Z hydrocarbon or CX Y -CX Z fatty acid each refers to a range of paraffin, n-paraffin, i-paraffin, monobranched i-paraffin, multibranched i-paraffin, hydrocarbon or fatty acid, where X Y and X Zis an achievable end - value integer, and the carbon numbers within such a range are those indicated by the end - value integer and, if present, any integer between the said end - values. However, in some cases, all paraffins, n - paraffins, i - paraffins, mono - branched i - paraffins, multi - branched i - paraffins, hydrocarbons or fatty acids with carbon numbers within the said range, especially at the endpoints or around them, may not necessarily exist (except when so explicitly indicated). On the other hand, by definition, isomers may include several compounds having the same carbon number. For example, C9 isomers may include methyloctanes (with different positions of the methyl branch), dimethylheptanes (with different positions of the two methyl branches), etc., and "C9 isomers" includes the total amount of all such variants. Typically, the total amount is meant as the weight or volume of all paraffins, n - paraffins, i - paraffins, mono - branched i - paraffins, multi - branched i - paraffins, hydrocarbons or fatty acids with carbon numbers defined each time. For example, C4 - C9 n - paraffins refer to any n - paraffins within the said range such as C4, C5, C6, C7, C8 and C9 n - paraffins, even if the content of C9 n - paraffin is 0. In other words, the total amount can be obtained by adding 0 (referring to the non - existent C9 n - paraffin) to the total weight of all other existing C4 - C9 n - paraffins.

[0034] Isomerization converts at least a certain amount of n - paraffins into i - paraffins, especially mono - branched i - paraffins. By further increasing the degree of isomerization, for example, by increasing the degree of hydro - isomerization as described below, more n - paraffins can be converted into i - paraffins, and mono - branched i - paraffins can be converted into multi - branched i - paraffins, such as di - branched, tri - branched i - paraffins, and even i - paraffins containing more than three branches.

[0035] As used in the context of this specification and the second reactor section, effective resolution refers to the cracking that produces non-gas (NTP) cracking products, particularly expressed as the ratio of the C8 - C14 hydrocarbon content in the hydrocracking effluent to the C8 - C14 hydrocarbon content in the second reactor section feed.

[0036] As used herein, the term renewable refers to compounds or compositions that can be obtained from, derivable from, or derived from plants and / or animals, and includes, in whole or in part, compounds or compositions that can be obtained from, derivable from, or derived from fungi and / or algae. As used herein, renewable compounds or compositions can include genetically engineered compounds or compositions. A renewable feedstock, ingredient, compound, or composition may also be referred to as a biological feedstock, ingredient, compound, or composition, or a feedstock, ingredient, compound, or composition of biological origin.

[0037] As used herein, the term fossil refers to compounds or compositions that can be obtained from, derivable from, or derived from naturally occurring non-renewable compositions, such as crude oil, petroleum / gas, shale oil / gas, natural gas, or coal deposits, and combinations thereof, and includes any hydrocarbon-rich deposits that can be utilized from surface / subsurface sources. The term recycle typically refers to recycled materials derived from non-renewable sources. For example, the term recycle may refer to recycled materials derived from waste plastics.

[0038] The above renewable, recycled, and fossil compounds or compositions are considered to be different from each other based on their origin and impact on environmental issues. Thus, they may be treated differently under the framework of laws and regulations. Typically, renewable, recycled, and fossil compounds or compositions are distinguished based on their origin and the information provided by their manufacturers.

[0039] Chemically, the renewable or fossil origin of any organic compound containing hydrocarbons can be determined by suitable methods for analyzing the carbon content from renewable sources, such as DIN 51637 (2014), ASTM D6866 (2020) or EN 16640 (2017). The above methods are based on the fact that carbon atoms of renewable or biological origin contain a larger number of unstable radiocarbon ( 14 C) atoms compared to carbon atoms of fossil origin. Thus, 12 C and 14 C isotope ratios can be analyzed to distinguish carbon compounds derived from renewable or biological sources or raw materials from those derived from non-renewable or fossil sources or raw materials. Thus, the specific ratios of the above isotopes can be used as "tags" to identify renewable carbon compounds and distinguish them from non-renewable carbon compounds. Isotope ratios do not change during the course of chemical reactions. Thus, isotope ratios 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 blends thereof. Numerically, the carbon content of biological origin can be expressed as the amount of carbon of biological origin in the material as a weight percentage of the total carbon (TC) in the material (in accordance with ASTM D6866 (2020) or EN 16640 (2017)). In this context, the term renewable preferably refers to a material having a carbon content of biological origin that exceeds 50 wt-%, particularly exceeds 60 wt-%, or exceeds 70 wt-%, preferably exceeds 80 wt-%, more preferably exceeds 90 wt-%, or exceeds 95 wt-%, and even more preferably about 100 wt-%, based on the total weight of carbon in the material (EN 16640 (2017)).

[0040] According to a first aspect, herein is provided a gasoline fuel component comprising n-paraffins, mono-branched i-paraffins and multi-branched i-paraffins, wherein the total amount of C4-C9 n-paraffins, C4-C9 mono-branched i-paraffins and C4-C9 multi-branched i-paraffins is more than 90 wt-% of the total weight of the gasoline fuel component, and the weight ratio of C8 i-paraffins to C8 n-paraffins is at least 4.0.

[0041] The gasoline fuel component is highly paraffinic and mainly comprises n-paraffins, mono-branched i-paraffins and multi-branched i-paraffins. The carbon number distribution may be relatively wide, but typically, since it is preferred that the gasoline fuel component is recovered as a distillation fraction, it is restricted by the boiling points of the hydrocarbons therein. In any case, the carbon number distribution of the paraffins in the gasoline fuel component typically covers at least three adjacent carbon numbers, preferably at least four adjacent carbon numbers, more preferably at least five adjacent carbon numbers within the range of C4-C9.

[0042] The gasoline fuel component is characterized by the total amount of C4-C9 n-paraffins, C4-C9 mono-branched i-paraffins and C4-C9 multi-branched i-paraffins, which together exceed 90 wt-% of the total weight of the gasoline fuel component. However, it should be noted that the above total amount is defined by adding together the amounts of any paraffins having the relevant carbon numbers (i.e., within the above range of carbon numbers including the end points) found by analysis. On the other hand, it should not be understood that the presence of paraffins having all carbon numbers within the above range is necessarily indicated.

[0043] C8 paraffin can be used in gasoline fuels and can be present in various amounts in the high-paraffin gasoline components, depending on the distillation end point used, especially for the recovery of the gasoline fraction. However, since the RON of n-C8 is as low as -20, its presence can have an adverse effect on the octane number of gasoline fuel components. For example, eliminating all C8 paraffins from the recovered gasoline fuel components by reducing the FBP of the gasoline fuel components causes an unacceptable yield reduction of the above components. Surprisingly, by controlling the weight ratio of C8i-paraffin to C8n-paraffin to be at least 4.0, preferably at least 4.5, more preferably at least 5.0, even more preferably at least 5.5, still more preferably at least 6.0, preferably at most 70, more preferably at most 60, even more preferably at most 50, still more preferably at most 40, typically at most 30, or at most 25, or at most 20, it has been found that it is possible to obtain components with good octane number without the need to eliminate the C8 paraffin content. Conversely, C8 paraffin can be incorporated in a significant amount, typically at least 1.0 wt-%, preferably at least 2.5 wt-%, more preferably at least 5.0 wt-%, even more preferably at least 5.5 wt-%, still more preferably at least 6.0 wt-%, or most preferably at least 7.0 wt-%, typically at most 50 wt-%, or at most 40 wt-%, or at most 30 wt-%, or at most 25 wt-%, for example 4.0 to 50 wt-%, or 4.5 to 50 wt-%, or 5.0 to 40 wt-%, without destroying the octane number of the component, provided that the ratio of C8i-paraffin to C8n-paraffin as defined above is met.The C8n-paraffin may be contained in the gasoline fuel component in a non-negligible amount, typically at least 0.1 wt-%, more preferably at least 0.3 wt-%, more preferably at least 0.5 wt-%, even more preferably at least 0.6 wt-%, while still having a good or sufficient octane number, provided that the ratio of C8i-paraffin to C8n-paraffin is as defined above. In fact, even more significant improvements can be seen compared to conventional paraffinic gasoline components. When the ratio of C8i-paraffin to C8n-paraffin is as defined above, the C8n-paraffin content may be 1.0 wt-% or more, 1.5 wt-% or more, 2.0 wt-% or more, 2.5 wt-% or more, or even 3.0 wt-% or more while still providing an acceptable octane number, as shown by the examples.

[0044] Generally, C7 paraffins are abundantly contained in high-paraffinic gasoline components due to the distillation process for recovering the gasoline fraction. Defining embodiments of the gasoline fuel component by its C7 paraffin content highlights interesting qualities. In certain embodiments, the amount of C7 paraffins, in total, in the gasoline fuel component is at least 15 wt-%, preferably at least 20 wt-%, such as in the range of 15 wt-% to 40 wt-%, or 15 wt-% to 35 wt-%, or 15 wt-% to 30 wt-%. C7 paraffins refer to the total amount of C7n-paraffins, C7 mono-branched i-paraffins, and C7 multi-branched i-paraffins. Nevertheless, the octane number of n-heptane, a C7n-paraffin, is 0, which reduces the RON and MON values of the gasoline fuel component and the final gasoline fuel composition.

[0045] Therefore, in order to improve the RON of gasoline fuel components, it is beneficial to have the highest possible i-C7 / n-C7 ratio. In certain embodiments, the weight ratio of C7i-paraffin to C7n-paraffin (i-C7 / n-C7 ratio) is at least 2.7, preferably at least 2.8, preferably at least 2.9, preferably at least 3.0, preferably at least 3.1, preferably at least 3.2, preferably at least 3.4. In high-paraffin compositions, such an i-C7 / n-C7 ratio has been found to be an indicator of particularly high-quality gasoline components, as shown by the examples. In practice, the upper limit of the above ratio is derived from a reasonable degree of isomerization, so the above ratio can be up to 5.0 or up to 10. Therefore, the above ratio can vary from 2.7 to 10, for example from 3.4 to 5.0. Conventional paraffinic gasoline fuel components, such as those derived from the hydrodeoxygenation of vegetable oils, tend to have a lower i-paraffin content, especially when the carbon number is low, such as C7.

[0046] Yet another single carbon number of interest is C6, where again, keeping the content of C6n-paraffin, n-hexane, low is beneficial for improving RON and also due to its properties that raise concerns for health and / or the environment. Thus, in certain embodiments, the C6n-paraffin content of the gasoline fuel component is up to 11 wt-%, up to 9 wt-%, up to 8 wt-% of the total weight of the gasoline fuel component, such as 0.5 wt-% to 11 wt-% or 0.5 wt-% to 8 wt-% of the total weight of the gasoline fuel component. The total amount of C6 paraffins in the gasoline fuel component is typically at least 10 wt-% and up to 40 wt-% of the total weight of the gasoline fuel component. The higher the total C6 paraffin content, the higher the absolute C6n-paraffin content tends to be, but in any case, in this gasoline fuel component, the weight ratio of C6i-paraffin to C6n-paraffin preferably exceeds 1.0.

[0047] C6 represents the typical carbon number of any hydrocarbon gasoline, but this gasoline component can be particularly advantageous due to its relatively high i-paraffin content, which can also be applied to C6 paraffins. In such embodiments, even if the C6 paraffins are abundant, the n-hexane content is not as high as to be a concern because of the high i-paraffin composition. The relatively high i-paraffin content relative to the n-paraffin content of paraffins with 6 carbon atoms can be given as the weight ratio of C6 i-paraffins to C6 n-paraffins. Thus, in certain embodiments, this gasoline fuel component can be characterized in that the weight ratio of C6 i-paraffins to C6 n-paraffins is at least 1.5, preferably at least 1.7, more preferably at least 2.0.

[0048] Preferably, this gasoline fuel component contains at least 0.5 wt-%, more preferably at least 1.0 wt-%, still more preferably 1.5 wt-%, even more preferably at least 3.0 wt-%, most preferably at least 5.0 wt-%, typically up to 10.0 wt-% of C4 n-paraffins, based on the total weight of the gasoline fuel component. Typically, the total C4 paraffin content in this gasoline fuel component is at least 1.0 wt-%, further at least 5.0 wt-% or at least 7.0 wt-%, typically up to 15 wt-%, based on the total weight of the gasoline fuel component. This gasoline fuel component can contain a non-negligible amount of C4 n-paraffins and / or total C4 paraffins without impairing the vapor pressure and / or other properties. A higher occupancy of C4 paraffins can make it possible to increase the yield of the gasoline fuel component, especially when the gasoline fuel component is recovered from a fractionation.

[0049] Typical embodiments of this gasoline fuel component may include at least C6, C7, and C8 paraffins. Considering the i-paraffin content relative to the n-paraffin content of C6 to C8 carbon atoms, these embodiments may be characterized in that the weight ratio of C6 to C8 i-paraffins to C6 to C8 n-paraffins is at least 2.7, preferably at least 2.8, more preferably at least 3.0. As seen in the examples, C6, C7, and C8 can be the most abundant carbon numbers in the gasoline fuel component in certain embodiments. Thus, the weight ratio of C6 to C8 i-paraffins to C6 to C8 n-paraffins represents such embodiments of this gasoline fuel component very well. Having such a high degree of isomerization within this carbon number range C6 to C8 is not at all typical in prior art gasoline cuts. Further, since the RON of n-C6 paraffin is 25, the RON of n-C7 paraffin is 0, and the RON of n-C8 paraffin is -20, their presence can have an adverse effect on the octane number of the gasoline fuel component. For example, by reducing the FBP of the component, eliminating all C8 paraffins, as well as all of C7 and C8 and even further C6 paraffins, causes an unacceptable yield reduction of the component. Surprisingly, it has been found that by controlling the weight ratio of C6 to C8 i-paraffins to C6 to C8 n-paraffins as specified, a component with good octane number can be provided without the need to eliminate or even further substantially minimize the content of C7 and C8 paraffins. Conversely, C6 to C8 paraffins can be incorporated in high amounts without destroying the octane number of the gasoline fuel component. Preferably, the total amount of C6 to C8 n-paraffins and C6 to C8 i-paraffins is at least 50 wt-%, more preferably at least 55 wt-%, even more preferably at least 58 wt-% of the total weight of the gasoline fuel component, and typically up to 95 wt-%, or up to 90 wt-%, or up to 85 wt-% of the total weight of the gasoline fuel component. Such a total amount of C6 to C8 n-paraffins and C6 to C8 i-paraffins in the gasoline fuel component can provide a significant improvement over conventional paraffinic gasoline components.

[0050] Another characteristic that correlates with the desired properties of the gasoline fuel component is the weight ratio of the total amount of C6-C9 multi-branched i-paraffins to the total amount of C6-C9 n-paraffins. According to certain preferred embodiments, the above weight ratio of C6-C9 multi-branched i-paraffins to C6-C9 n-paraffins is at least 0.2, preferably at least 0.3, more preferably at least 0.4, and even more preferably at least 0.5. The above ratio may be up to 1.5 or even up to 2.0. A high weight ratio of C6-C9 multi-branched i-paraffins to C6-C9 n-paraffins significantly improves the RON of the paraffinic gasoline fuel component. Compared with mono-branched i-paraffins, multi-branched i-paraffins are more effective in compensating for the low RON of n-paraffins. Conventional gasoline components obtained from the hydrodeoxygenation of vegetable oils have a lower multi-branched i-paraffin content. The octane number of n-heptane is 0, but the RON and MON of both n-C8 and n-C9, i.e., n-octane and n-nonane, are even lower and less than 0.

[0051] Highly isomerized gasoline fuel components have been found to provide advantages related to octane number over n-paraffin compositions. Thus, according to certain preferred embodiments, the gasoline fuel component comprises at least 50 wt-%, preferably at least 55 wt-%, more preferably at least 60 wt-%, even more preferably at least 65 wt-% of C4-C9 i-paraffins based on the total weight of the gasoline fuel component, and / or at least 5 wt-%, preferably at least 6 wt-%, more preferably at least 7 wt-%, even more preferably at least 10 wt-% or at least 11 wt-% of C6-C9 multi-branched i-paraffins based on the total weight of the gasoline fuel component. Thus, in such embodiments, the gasoline fuel component is predominantly i-paraffin based, and the notable portion of the above i-paraffins may contain two or more branches. Gasoline fuel components having such contents of C4-C9 i-paraffins and / or C6-C9 multi-branched i-paraffins have a high i-paraffin content, but significantly improve the RON of the (high paraffin-based) gasoline fuel component compared to conventional gasoline components derived from hydrodeoxygenation of vegetable oils which may have a low multi-branched i-paraffin content, especially in the case of the lower carbon numbers described above.

[0052] The research method octane number and motor method octane number, RON and MON, can be measured for neat gasoline components or gasoline components blended with another gasoline component having a known octane number, and are given as bRON and bMON, respectively. As used throughout this specification, the acronyms RON, bRON, MON, and bMON refer to the corrected measured RON, bRON, MON, and bMON, i.e., the corrected values obtained after subtracting 0.2 from the measured value (in accordance with section 5.6 of EN228:2012 as amended in 2017). Throughout this specification, clean research method and motor method octane numbers are intended, i.e., obtained without using octane number enhancing additives. Standard methods for RON and MON measurements are described, for example, in ASTM D2699 / D2700. The measurement and calculation of bRON are known in the art and are disclosed, for example, in U.S. Patent No. 4,244,704. In the experimental section of the present disclosure, gasoline fuel components according to the present disclosure were studied in blends with typical gasoline components. Surprisingly, the bRON and bMON results of the gasoline fuel components according to the present disclosure were significantly better than those of another renewable paraffinic gasoline component used as a reference in the above experiments. When the octane number of the reference gasoline component is low, its use in the blend is restricted because if its amount in the gasoline composition is too large, the octane number will fall below the target. Therefore, a greater share of this gasoline fuel component can be incorporated into the gasoline fuel composition without compromising the target octane as compared to the above reference renewable gasoline component. Thus, according to certain embodiments, the gasoline fuel component has a bRON of at least 51, preferably at least 55. According to certain embodiments, the gasoline fuel component has a bMON of at least 48, preferably at least 50, and more preferably at least 55.

[0053] The inventors have also found that this gasoline fuel component containing a high content of paraffins within the carbon number range C4 - C9 can be very beneficial compared to prior art gasoline components for several reasons. For example, the high paraffin - based gasoline fuel component of the present disclosure naturally has a low total content of compounds other than paraffins. For example, the total content of aromatics, olefins, and naphthenes is typically less than 5.0 wt - %, often less than 4.0 wt - % of the total weight of the gasoline fuel component, and in many cases at most 3.0 wt - %. Among these, the total content of aromatics is typically less than 3.0 wt - % of the total weight of the gasoline fuel component, and often less than 2.0 wt - %. The low aromatic content contributes, for example, to a reduction in deposit formation in engines and injectors. Overall, the incorporation of the high paraffin - based gasoline fuel component into a blend supports meeting standards such as EN 228, especially considering the restrictions on aromatics and benzene. The high paraffin content can also provide easy biodegradability. Furthermore, the high paraffin - based gasoline fuel component can provide better performance to the end - user regarding combustion and / or emissions. Additionally, the blendability of this gasoline fuel component with other typical gasoline components is very good. Moreover, the high paraffin - based gasoline fuel component is more stable or more inert, for example, during storage and blending, compared to components with a high content of non - paraffin compounds, especially olefins, that can react in the component or in its gasoline fuel composition to form high - molecular - weight precipitates, i.e., gums. Typically, the total content of olefins is less than 1000 vol - ppm of the total gasoline fuel component weight. Also, aromatics are particularly susceptible to the effects of instability with increasing size and concentration of aromatics, for example, the tendency to deposit under stress caused by oxidation and molecular growth of aromatics may be higher. The improved stability is a particularly desirable property, for example, for hybrid vehicles that use another primary power source such as electricity or gas and gasoline only as a secondary fuel that is held in the fuel system for a long time. Furthermore, certain ranges of paraffins, such as within the range C4 - C9, are beneficial to the final product properties when blended with other typical gasoline components compared to neat or pure components, such as neat n - naphthenes.

[0054] Thus, according to certain preferred embodiments, in this gasoline fuel component, the total amount of C4-C9 n-paraffins, C4-C9 mono-branched i-paraffins and C4-C9 multi-branched i-paraffins is more than 93 wt-%, preferably more than 95 wt-%, more preferably 95-99 wt-% of the total weight of the gasoline fuel component.

[0055] When the content of paraffins within the carbon number range C4-C9 is high, the total amount of any hydrocarbon having three or fewer carbon atoms (C3-hydrocarbons), i.e., C1-C3 hydrocarbons, is low, typically at most 4.0 wt-%, or at most 3.5 wt-%, or at most 3.0 wt-% of the total weight of the gasoline fuel component. By restricting the presence of light hydrocarbons, i.e., hydrocarbons having three or fewer carbon atoms, the handling of components and any products such as its gasoline fuel composition is improved.

[0056] By further studying the paraffins within the carbon number range C4 - C9 of the gasoline fuel component, the inventors also defined the average carbon number of n - paraffins and i - paraffins within the above carbon number range. According to a specific embodiment of the gasoline fuel component, the average carbon number of C4 - C9 n - paraffins is at most 6.0, preferably at most 5.6. Preferably, the average carbon number is between 5.0 and 6.0 or within the range of 5.0 - 6.0. Compared with the average carbon number of C4 - C9 i - paraffins in the gasoline fuel component, C4 - C9 n - paraffins have an average carbon number that is at least 0.5 units lower, preferably at least 0.6 units lower, than the average carbon number of the corresponding C4 - C9 i - paraffins. It has been found that this contributes to the octane number such that the lower the average carbon number of C4 - C9 n - paraffins, the higher the RON of the gasoline fuel component. Since it has been found that the average carbon number of i - paraffins is higher, according to a specific embodiment, the average carbon number of C4 - C9 i - paraffins is greater than 6.0, preferably at least 6.2, more preferably within the range of 6.2 - 8.0. The RON of n - paraffins tends to increase as the carbon number decreases. For example, the RON of n - C8 and n - C9 is - 20 or less, the RON of n - C7 is 0, the RON of n - C6 is 25, the RON of n - C5 is 62, and the RON of n - C4 is 94. Furthermore, the RON of paraffins tends to increase as the degree of branching increases. Compared with n - paraffins of the same carbon number, monobranched i - paraffins have a somewhat higher octane number, and multi - branched i - paraffins have a significantly higher octane number. For example, reducing the average carbon number of paraffins in the C4 - C9 range in the component by lowering the FBP of the component causes an unacceptable decrease in yield. Also, thoroughly increasing the degree of branching is uneconomical and unnecessary. Surprisingly, by controlling the average carbon number of C4 - C9 n - paraffins and / or C4 - C9 i - paraffins as specified above, it is possible to provide a gasoline fuel component having a good octane number without excessively reducing the FBP or thoroughly increasing the degree of branching.

[0057] This gasoline fuel component can be obtained from renewable raw materials that provide a high bio-content in their products by a process that will be defined in detail later. The carbon content of biological origin can be defined for any feasible composition according to EN 16640 (2017). According to certain embodiments, the carbon content of biological origin of the gasoline fuel component is at least 50 wt-%, preferably at least 70 wt-%, more preferably at least 90 wt-%, or at least 95 wt-%, or even about 100 wt-% based on the total weight of carbon (TC) in the gasoline fuel component. This gasoline fuel component contributes to the bio-content of the total gasoline fuel composition and advantageously increases its bio-content.

[0058] As shown by the examples, this gasoline fuel component can be obtained as a fraction recovered from a process developed for the production of high-quality liquid transport fuel components, particularly optimized for the production of renewable and / or sustainable aviation fuels. In certain preferred embodiments, an aviation fuel component is recovered from the fraction in addition to the above gasoline fuel component, and both can be used as liquid transport fuel components. The combined recovery of the gasoline fuel component and the aviation fuel component provides a more valuable product from the efficient use and purification of the feedstock to the process. Generally, gasoline fuels and aviation fuels can have relatively little overlap with respect to boiling point and hydrocarbon distribution. Thus, this gasoline fuel component and the (renewable) aviation fuel component can be recovered as subsequent cuts from a fractionation, for example by distillation. Furthermore, process selections that improve the quality of the aviation fuel component, such as the hydrocracking of an isomerized paraffin stream, also improve the quality of the gasoline fuel component, particularly blendability, octane number, and combustion characteristics.

[0059] The beneficial properties of this gasoline fuel component, particularly the high i-paraffin / n-paraffin ratio in the lower-carbon-number paraffins, can be brought about by the production process and the feedstock to the production process. The gasoline fuel component can be obtained directly from the product recovery of the production process or can be obtained.

[0060] In certain embodiments, the gasoline fuel component can be obtained or is obtained by a process comprising hydrogenating and deoxygenating an oxygenate feedstock typically containing vegetable oil, animal fat, and / or microbial oil, and optionally subsequently providing a paraffinic hydrocarbon feedstock preferably obtained by gas-liquid separation and / or a paraffinic feedstock fractionation; subjecting the paraffinic hydrocarbon feedstock to at least hydroisomerization, preferably to hydroisomerization and hydrocracking, subsequently subjecting it to fractionation, and recovering at least the gasoline fuel component from the fractionation. The feedstocks and process steps, particularly the paraffinic hydrocarbon feedstock, hydroisomerization and optional hydrocracking, and fractionation are preferably as further defined herein. According to certain preferred embodiments, this gasoline fuel component provides a paraffinic hydrocarbon feedstock containing at least 60 wt-% paraffins based on the total weight of the paraffinic hydrocarbon feedstock, with a maximum of 30 wt-% of the paraffins in the paraffinic hydrocarbon feedstock being i-paraffins, in a first reaction section, preferably a first reactor, subjecting the paraffinic hydrocarbon feedstock to hydroisomerization in the presence of a hydroisomerization catalyst to obtain a hydroisomerization effluent, subjecting a second reaction section feedstock containing at least a portion of the hydroisomerization effluent to hydrocracking in a second reaction section, preferably a second reactor, in the presence of a hydrocracking catalyst to obtain a hydrocracking effluent, subjecting the hydrocracking effluent, and optionally (at least) a portion of the hydroisomerization effluent, to fractionation to recover at least the gasoline fuel component and optionally an aviation fuel component from the fractionation, and can be obtained or is obtained by a process comprising.

[0061] Optionally, other products such as diesel fuel components can also be recovered.

[0062] Preferably, the process has a T5 temperature (5 vol-% recovery, EN ISO 3405-2019) of preferably 270 °C or higher and further includes recovering a recycle stream containing C16n-paraffin, if desired, from the fractionation. The recycle stream may be included in at least a part of the hydroisomerization effluent or may form at least a part of the hydroisomerization effluent that is subjected to hydrocracking in a second reaction section, preferably a second reactor. In other words, the recycle stream can be subjected to hydrocracking in a second reaction section, preferably a second reactor, as part of the second reaction section feed. The recycle stream may include at least a part of the fractionation bottoms. In embodiments where the recycle stream is separated, in particular in embodiments where the second reaction section feed to hydrocracking includes, in addition to the recycle stream, a further portion of the hydroisomerization effluent, the yield of the desired liquid fuel components can be further optimized. In embodiments where the recycle stream is separated, diesel fuel components can be conveniently recovered by separating a part from the recycle stream.

[0063] In this process, the paraffinic hydrocarbon feed contains at least 60 wt-%, preferably at least 70 wt-%, more preferably at least 80 wt-%, even more preferably at least 90 wt-% paraffin, based on the total weight of the paraffinic hydrocarbon feed. The paraffinic hydrocarbon feed of the present disclosure may even contain at least 95 wt-% paraffin, based on the total weight of the paraffinic hydrocarbon feed, or may consist essentially of paraffin. The paraffinic hydrocarbon feed of the present disclosure may contain small amounts, preferably less than 5 wt-%, more preferably less than 1 wt-% olefins, as well as small amounts of aromatics and / or naphthenes, based on the total weight of the paraffinic hydrocarbon feed.

[0064] The advantage of using a paraffinic hydrocarbon feedstock in the process of the present disclosure is that paraffins are isomerized under relatively mild conditions more readily when subjected to hydrogen isomerization, for example, compared to cyclic hydrocarbons. Also, paraffins decompose under mild conditions more readily when subjected to hydrocracking, which helps to reduce the formation of light gases.

[0065] In this process, a paraffinic hydrocarbon feedstock containing at least 60 wt-% paraffins of the total weight of the paraffinic hydrocarbon feedstock, with at most 30 wt-% of the paraffins being i-paraffins, can be obtained from paraffin hydrotreated effluents such as hydrodeoxygenation (HDO) effluents, paraffinic Fischer-Tropsch (FT) effluents, or combinations 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 a paraffinic feedstock fractionation. For example, paraffinic FT effluents of fossil origin are readily available (in addition to FT effluents of renewable origin), but preferably, the paraffinic hydrocarbon feedstock of the present disclosure is at least partially renewable, i.e., contains components of biological origin.

[0066] Preferably, the paraffinic hydrocarbon feedstock of the present disclosure comprises, or consists essentially of, the hydrodeoxygenation (HDO) effluent or a portion thereof from the catalytic hydrodeoxygenation (catalytic HDO) of an oxygenated hydrocarbon feedstock, such as a de-aerated hydrodeoxygenation effluent or a portion thereof. Preferably, the oxygenated hydrocarbon feedstock comprises at least one or more of vegetable oils, animal fats, and / or microbial oils. This type of paraffinic hydrocarbon feedstock tends to have a relatively narrow carbon number distribution and, thus, may benefit more from being subjected to the process of the present invention, for example, as compared to an FT-based feedstock, which typically has a substantially Gaussian distribution of hydrocarbon chains and a broad carbon chain length distribution. Typically, providing a paraffinic hydrocarbon feedstock involves subjecting an oxygenated hydrocarbon feedstock to hydrodeoxygenation in the presence of a hydrodeoxygenation catalyst to obtain a hydrodeoxygenation effluent, and then subjecting the hydrodeoxygenation effluent to gas-liquid separation and, optionally, to paraffinic feedstock fractionation to obtain a de-aerated hydrodeoxygenation effluent or a fraction thereof as the paraffinic hydrocarbon feedstock. Hydrodeoxygenation can be carried out as described in prior art publications, such as Finnish Patent No. 100248, European Patent Application Publication No. 1741768, European Patent No. 2155838, or Finnish Patent 129220.

[0067] Generally, in the context of the present disclosure, the hydroisomerization (HI) of a paraffinic hydrocarbon feed in the first reaction section / reactor is operated such that the isomerization reaction is dominant while the cracking reaction is controlled or suppressed. Typically, HI in the first reaction section / reactor is carried out at 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, an H2 partial pressure at the inlet of the first reaction section / 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 an H2 to paraffinic hydrocarbon feed ratio in the range of 10 to 2000, preferably 50 to 1000 normal liters H2 / liter paraffinic hydrocarbon feed. The hydroisomerization can be carried out as described in prior art publications, for example, Finnish Patent No. 100248, European Patent Application Publication No. 1741768, European Patent No. 2155838 or Finnish Patent 129220. The degree of HI can be increased by at least one or more of decreasing the WHSV, increasing the temperature, and / or increasing the pressure. When using a fresh HI catalyst, higher HI conditions can be achieved at lower temperatures and / or pressures and / or using a higher WHSV, and towards the end of the HI catalyst life, higher temperatures and / or pressures and / or a lower WHSV may be required even to achieve moderate HI.In this context, an HI that produces a liquid effluent having a total i-paraffin content of 50 to 85 wt-% and a multi-branched i-paraffin content of up to 25 wt-%, or a total i-paraffin content of 85 to 95 wt-% and a multi-branched i-paraffin content of 25 to 55 wt-%, or a total i-paraffin content of at least 95 wt-% and a multi-branched i-paraffin content exceeding 55 wt-%, as wt-% of paraffin in the liquid effluent, is generally regarded as a low or medium or high HI, respectively. However, these content ranges are only for indicating the index, are somewhat overlapping, and may vary depending on the case.

[0068] Generally, the hydrocracking in the second reaction section / reactor is operated such that reactions that particularly enhance the degree of effective cracking, not only for cracking reactions, especially C8 - C14 hydrocarbons but also for lighter non-gaseous hydrocarbons, are more abundant than the hydroisomerization in the first reaction section / reactor. Preferably, the cracking reaction, especially the reaction that enhances the degree of effective cracking, is dominant in the hydrocracking in the second reaction section / reactor, but generally there is no excessive cracking and no excessive fuel gas formation. Typically, the hydrocracking in the second reaction section / reactor is carried out at a temperature in the range of 200°C to 450°C, preferably 220°C to 430°C, more preferably 280°C to 350°C, a pressure in the range of 0.4 MPa to 8 MPa, preferably 1 MPa to 7 MPa, an H2 partial pressure at the inlet of the second reaction section / reactor in the range of 0.4 MPa to 8 MPa, preferably 1 MPa to 7 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, even more preferably 0.5 to 1.5 kg of the second reactor feed / kg catalyst / hour, and an H2 to second reactor feed ratio in the range of 10 to 2000, preferably 50 to 1000 normal liters H2 / liter of the second reactor feed.

[0069] Preferably, the hydrogen isomerization catalyst is a non-sulfided dual-functional hydrogen isomerization catalyst, and the hydrocracking catalyst is a non-sulfided dual-functional hydrocracking catalyst. Preferably, the non-sulfided dual-functional catalyst comprises at least one or more metals selected from the noble metals of Group VIII, more preferably at least one or more metals selected from Pt and / or Pd, and at least one or more acidic porous materials. The non-sulfided dual-functional catalyst does not require sulfiding during operation to maintain activity, and thus can keep the sulfur content of various process streams and products low, and is preferred because less efficient H2S separation and recovery is required. In particular, a non-sulfided dual-functional catalyst containing a noble metal can be active at a lower temperature and can exhibit higher selectivity towards the isomerization reaction compared to a sulfided catalyst, but is sensitive to deactivation by H2S. In particular, in the hydrocracking reaction in the second reaction section / reactor, the dual-functional HC catalyst has at least some isomerization activity in addition to the cracking activity and can be particularly efficient in effective cracking, which is beneficial. As a further advantage, it has been found that a dual-functional hydrocracking catalyst containing at least one or more metals selected from Group VIII noble metals, preferably Pt and / or Pd, provides high activity at a relatively low temperature compared to an HC catalyst containing non-noble metals, and thus provides better control of thermal cracking. At low temperatures, the thermodynamic equilibrium tends to shift towards dearomatization, thus reducing the formation of aromatics by side reactions. By providing a dual-functional HC catalyst in the second reaction section / reactor, it can also be achieved that the isoparaffin content (wt-% isoparaffin of the total weight of paraffins) in the hydrocracking effluent is not necessarily significantly lower than, or may be the same as or even higher than, that in the hydrogen isomerization effluent.

[0070] According to certain preferred embodiments, the gasoline fuel component is obtained by subjecting an oxygenated hydrocarbon feedstock containing at least one or more of vegetable oil, animal fat and / or microbial oil to hydrodeoxygenation followed by vapor-liquid separation to provide a paraffinic hydrocarbon feedstock containing at least 60 wt-% paraffin based on the total weight of the paraffinic hydrocarbon feedstock, with a maximum of 30 wt-% of the paraffins in the paraffinic hydrocarbon feedstock being i-paraffins, In a first reaction section, preferably a first reactor, subjecting the paraffinic hydrocarbon feedstock to hydroisomerization in the presence of a hydroisomerization catalyst to obtain a hydroisomerization effluent, Subjecting a second reaction section feedstock, which includes at least a portion of the hydroisomerization effluent and optionally a recycle stream, to hydrocracking in a second reaction section, preferably a second reactor, in the presence of a hydrocracking catalyst to obtain a hydrocracking effluent, Subjecting the hydrocracking effluent to fractionation to recover at least a gasoline fuel component, and optionally an aviation fuel component, and / or preferably a recycle stream having a T5 temperature (5 vol-% recovery, EN ISO3405-2019) of 270 °C or higher, and can be obtained by a process comprising

[0071] The predominant component in the paraffinic hydrocarbon feedstock is n-paraffin. However, the presence of a certain amount of i-paraffin in the paraffinic hydrocarbon feedstock can still be beneficial. Compared to a similar feedstock that does not contain an i-paraffin content, a paraffinic hydrocarbon feedstock containing a certain amount of i-paraffin can achieve a hydroisomerization effluent with a higher content of multi-branched i-paraffins.

[0072] Preferably, the paraffinic hydrocarbon feedstock of the present disclosure comprises hydrocarbons having a carbon number in the range of C12 - C30, more preferably in the range of C14 - C22, at least 70 wt-%, preferably at least 80 wt-%, more preferably at least 90 wt-% of the total weight of the paraffinic hydrocarbon feedstock. These feedstocks enable good yields of two or more fuel components of different types and are readily available from conventional hydrodeoxygenation processes of vegetable oils containing fatty acids, animal fats, and / or microbial oils. Heavier paraffinic feedstocks can be obtained, for example, from the HDO of oils from energy crops such as Brassica species, algal oils, crude tall oil (CTO), tall oil fatty acids (TOFA), and / or tall oil pitch (TOP).

[0073] The presence of multi-branched i-paraffins in the hydroisomerization effluent can be considered beneficial as it can beneficially contribute to the degree of effective cracking in the hydrocracking step. In particular, when the desired degree of effective cracking for not only C8 - C14 hydrocarbons but also lighter non-gaseous hydrocarbons is achieved in the hydrocracking step under milder operating conditions, excessive cracking is avoided and the formation of gaseous hydrocarbons can be reduced. Also, an increase in the content of multi-branched i-paraffins in the hydroisomerization effluent can be considered beneficial in that it provides improved RON for gasoline fuel components and improved low-temperature properties for at least one or more additional fuel components that may be recovered as desired, such as aviation fuel components and / or diesel fuel components. Without being bound by any theory, multi-branched i-paraffins are more likely to form two branched paraffin molecules upon cracking in the hydrocracking step instead of one branch and one n-paraffin, and thus it is considered that the i-paraffin content of the hydrocracking effluent increases relative to the n-paraffin content. The same can be seen downstream of the product recovered from the fractionation and in the recycle stream that may be recovered as desired.

[0074] According to certain embodiments, the first reaction section for hydrogen isomerization and the second reaction section for hydrocracking may be arranged in one and the same reactor, for example, in separate catalyst beds equipped with suitable devices therefor. According to certain other embodiments, the first reaction section for hydrogen isomerization is in a first reactor and the second reaction section for hydrocracking is in a second reactor. Having a hydrogen isomerization section in the first reactor and a hydrocracking section in the second reactor provides advantages in process design, process control, and maintenance.

[0075] Preferably, at least a portion of the hydrogen isomerization effluent fed to the hydrocracking comprises at least 50 wt-%, more preferably at least 60 wt-%, even more preferably at least 70 wt-%, still more preferably at least 80 wt-% of isoparaffins based on the total amount of paraffins in at least a portion of the hydrogen isomerization effluent, and optionally at least 5 wt-%, preferably at least 10 wt-%, more preferably at least 15 wt-%, still more preferably at least 20 wt-%, typically up to 70 wt-% of multi-branched isoparaffins based on the total amount of paraffins in at least a portion of the hydrogen isomerization effluent. Typically, at least a portion of the hydrogen isomerization effluent has a cloud point of less than 0 °C, preferably less than -5 °C, more preferably less than -8 °C, still more preferably less than -10 °C, or less than -15 °C (ASTM D5771-17).

[0076] Hydrocracking of at least a portion of the hydrogen isomerization effluent increases the yield of non-gaseous cracking products, especially C8 - C14, but also increases the yield of lighter non-gaseous hydrocarbons that contribute to the yield of gasoline fuel components. Since the feed to the hydrocracking can contain a high i-paraffin content and a high multi-branched i-paraffin content, the inventors have found that hydrocracking can produce additional i-paraffins without excessive cracking to lower value light C1 - C3 hydrocarbons and instead reduce their amount.

[0077] The advantageous hydrocarbon composition of this gasoline fuel component is demonstrated in the end use as beneficial combustion in the engine, particularly with respect to the carbon number distribution and the content of i-paraffins and n-paraffins. When studied under laboratory conditions, the properties that correlate with the desired properties of the fuel are, for example, the shape of the distillation curve and the distillation characteristics. The temperatures of T10 and T90 reported in the examples and the difference between them immediately reveal to those skilled in the art the suitability of the gasoline for a spark ignition engine and the predicted performance in a spark ignition engine. Thus, according to a particular embodiment, herein, the difference between the T90 temperature (90 vol-% recovery, ASTM D7096-19) and the T10 temperature (10 vol-% recovery, ASTM D7096-19) is at least 60 °C, more preferably at least 70 °C, even more preferably at least 80 °C or at least 100 °C, for example in the range of 60 to 140 °C, and a gasoline fuel component is provided. Preferably, the gasoline fuel component has a T90 temperature (90 vol-% recovery, ASTM D7096-19) in the range of 95 to 150 °C, preferably in the range of 95 to 140 °C, more preferably in the range of 95 to 130 °C, in order to positively contribute to the octane number of the gasoline fuel component and enable the recovery of an aviation fuel component in high yield from the same production process.

[0078] Fractionation such that C8i - paraffins are recovered in the gasoline fuel component and C8n - paraffins having higher boiling points are recovered mainly in the aviation fuel component contributes to and / or can further increase the high weight ratio of C8i - paraffins to C8n - paraffins in the gasoline fuel component. By carefully selecting the cut - point in fractionation, the recovery of C8n - paraffins in the gasoline fuel component can be reduced without still significantly reducing the yield of the gasoline component. In this way, a gasoline fuel component having an even very high weight ratio of C8i - paraffins to C8n - paraffins can be obtained without the need to overly or radically increase the degree of branching. Other properties that the gasoline component follows are related to volatility, vapor pressure and flash point. Typical measures reflecting the above properties include E70 and E150 values. In the case of a gasoline composition, the E70 value defines the percentage (vol - %) evaporated at 70 °C at standard atmospheric pressure. The standardized methods for determining the E70 as well as the E100 and E150 values of a gasoline composition are defined in EN ISO3405:2011. Due to the carbon number distribution and content of i - paraffins and n - paraffins in the gasoline fuel component, the blend is not restricted by the vapor pressure.

[0079] According to a further aspect, the gasoline fuel component can be used in a gasoline fuel composition. The higher i-paraffin content and improved i-paraffin profile contribute to an improved RON, which allows the gasoline fuel component to be incorporated into gasoline fuel in a greater amount compared to, for example, biomass-derived transport fuels suitable for use in currently commercially available spark ignition engines (such currently commercially available fuels have a lower RON). Compared to aromatic-containing blend components, the gasoline fuel component causes less emissions. Further, the gasoline fuel component can help increase the bio-content of the gasoline fuel composition. Further, each of the increase in i-paraffin content, the increase in the weight ratio of i-paraffin to n-paraffin, and the increase in the weight ratio of multi-branched i-paraffin to n-paraffin helps to reduce the viscosity of the gasoline fuel component, thereby improving the mixing and blendability with further components included in the gasoline fuel composition.

[0080] Currently, compared to ethanol, the dominant bio-component blended in gasoline compositions, the gasoline component has low hygroscopicity. Further, in the distillation of gasoline blends, ethanol as a blend component turns to a steeper gradient at about 70 °C, thus creating a significant angle with respect to the distillation curve, leading to issues in meeting the requirements of gasoline compositions as specified in, for example, EN228:2012 as amended in 2017, whereas the gasoline fuel component in the blend can provide a substantially linear distillation curve. In contrast to ethanol and other oxygenates, there are no regulatory blend limits for paraffinic blend components such as the gasoline fuel component. Accordingly, the gasoline fuel component is a highly desirable alternative blend component for gasoline fuel and is expected to be beneficial for both the manufacture of gasoline fuel compositions and end-users.

[0081] The beneficial vapor pressure characteristics of this gasoline fuel component enable the use of less expensive and lighter blend components such as butane in the gasoline fuel composition, which would not be an option if another component with a higher vapor pressure, such as ethanol, were used as the bio-component.

[0082] When used in a gasoline fuel composition, the gasoline fuel component may be blended with at least one or more additional components. These may be derived from various sources and / or hydrocarbon refining processes, and are typically recovered therefrom by distillation. Examples of such processes include FCC, reforming, alkylation, pyrolysis, steam cracking, hydrodeoxygenation, hydrodesulfurization, isomerization, or combinations thereof. Thus, in addition to the gasoline fuel component, the gasoline fuel composition may contain at least one or more of alcohols, ethers, and / or hydrocarbon cuts, preferably methanol, ethanol, propanol, i-propanol, butanol, i-butanol, tert-butanol, pentanol, i-pentanol, MTBE, ETBE, DIPE, TAME, TAEE, butane, alkylate gasoline, isomerate, raffinate, FCC gasoline, reformate, pygas, and / or light straight run (LSR) gasoline. With respect to high octane number and carbon content of biological origin, particularly good gasoline fuel compositions can be obtained when the maximum amount of oxygenated gasoline fuel component of biological origin, preferably ethanol of biological origin, allowed by the required maximum oxygen content and the maximum amount of renewable gasoline fuel component allowed by the required minimum octane number are blended with fossil hydrocarbon cuts. The gasoline fuel composition may further contain at least one or more additives, preferably at least one or more of antioxidants, stabilizers, surfactants, corrosion inhibitors, friction modifiers, metal deactivators, and / or fuel dyes. Blends containing three or more additional components are typical. Exemplary gasoline fuel compositions, to mention some exemplary gasoline fuel compositions, may include the gasoline fuel component, ethanol, alkylate gasoline, antioxidant and stabilizer, or the gasoline fuel component, ethanol, LSR gasoline, antioxidant, stabilizer and surfactant, or the gasoline fuel component, MTBE, pygas, FCC gasoline, antioxidant, stabilizer, friction modifier and surfactant.

[0083] According to certain embodiments, by blending the gasoline fuel component, the gasoline fuel composition meets the requirements for gasoline fuel as defined in Directive 2009 / 30 / EC and, optionally, EN228:2012 as amended in 2017.

[0084] According to certain embodiments, the gasoline fuel composition comprises the gasoline fuel component in an amount of 1 to 25 vol-%, preferably 1 to 20 vol-%, of the total volume of the gasoline fuel composition. When the gasoline fuel component has a high bio-content, the gasoline fuel component alone can provide a significant bio-content to the gasoline fuel composition. The bio-content can be further enhanced when the gasoline fuel composition comprises the gasoline fuel component in an amount of 1 vol-% to 25 vol-%, preferably 1 vol-% to 20 vol-%, of the total volume of the gasoline fuel composition and up to 20 vol-% or up to 10 vol-% of ethanol, preferably bio-ethanol, of the total volume of the gasoline fuel composition. In the case of such a gasoline fuel composition, even at a height of 45 vol-% of the components, it can be renewable by providing a bio-origin carbon content (EN 16640 (2017)) exceeding 40 wt-% based on the total weight of carbon (TC) in the gasoline fuel component. A particularly promising gasoline fuel composition comprises the gasoline fuel component in an amount of about 10 vol-% of the total volume of the gasoline fuel composition and about 10 vol-% of bio-ethanol.

[0085] In addition to its usefulness in gasoline fuel compositions, this gasoline fuel component is suitable for a wide variety of other applications, for example in raw materials for industrial conversion processes, preferably in pyrolysis raw materials and / or catalytic cracking raw materials, in solvents, carriers, dispersant compositions, demulsifiers, extractants, surfactants, degreasing compositions, detergents, thinners, penetrating oils, anticorrosion compositions, multipurpose oils, in metalworking, in agriculture, in construction, in electronic devices, in medical instruments, in compositions for the automotive, electrical, textile, packaging, paper and / or pharmaceutical industries, and / or in the manufacture of intermediates therefor. The high isoparaffin to n-paraffin ratio of this gasoline fuel composition can reduce viscosity and improve pumping and mixing characteristics, as well as blendability, which are generally desired and beneficial properties for a wide range of applications, particularly those involving spraying, injection and / or mixing with other components. Due to generally meeting the most important specifications of light naphtha and / or gasoline commonly used as large amounts of industrial raw materials, this gasoline fuel composition can be used in the same applications without the need to modify existing equipment or facilities. The use of this gasoline fuel component is particularly preferred in pyrolysis raw materials and / or catalytic cracking raw materials for producing olefinic monomers, particularly ethylene and / or propylene, as the very low cyclic content helps to reduce the formation of coke-forming aromatics, the very high paraffin content helps to improve the conversion to light olefins even under less severe cracking conditions, and the high i-paraffin content is expected to favorably contribute to the production of the preferred propylene to ethylene product ratio in these processes.

[0086] Schematic presentation of the process Figure 1 schematically shows a process according to an exemplary embodiment for producing the present gasoline fuel component. In Figure 1, an oxygenated hydrocarbon feed 110 is supplied to an HDO reactor 120, where it is subjected to hydrodeoxygenation in the presence of an HDO catalyst 130 to obtain a hydrodeoxygenation effluent (HDO effluent) 140. The obtained HDO effluent 140 is subjected to gas-liquid separation 150 to separate a compound 160 that is gaseous at least at NTP from the HDO effluent, obtaining 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 supplied, in Figure 1, to a first reactor 180, where the degassed HDO effluent 170 is subjected to hydroisomerization in the presence of a hydroisomerization catalyst 190 to obtain a hydroisomerization effluent (HI effluent) 200. The obtained HI effluent 200 is subjected to gas-liquid separation 210 to separate a compound 220 that is gaseous at least at NTP from the HI effluent 200, obtaining a degassed HI effluent 230. In Figure 1, the degassed HI effluent 230 is supplied to a distillation unit 240 that may include a single column or a prefractionation and a main distillation column, from which several streams or cuts are obtained. From the distillation in Figure 1, a gasoline fuel component 250, as well as an aviation fuel component 260 and / or a diesel fuel component 270 are recovered. Further, a recycle stream 280 having a T5 boiling point of 270 °C or higher is separated in Figure 1. A second reaction section feed containing the recycle stream 280 as at least a part of the HI effluent is supplied, in Figure 1, to a second reactor 290, where it is subjected to hydrocracking in the presence of a hydrocracking catalyst 300 to obtain a recycle effluent (hydrocracking effluent) 310. In Figure 1, the recycle effluent 310 is subjected to gas-liquid separation 320 to separate a compound 330 that is gaseous at least at NTP from the recycle effluent 310, obtaining a degassed recycle effluent 340. The degassed recycle effluent 340 is then supplied, in Figure 1, as a co-feed with the degassed HI effluent 230 to the distillation unit 240 for fractionation.In certain embodiments, yet another portion of the HI effluent 200 or 230 may be supplied as a co-feed 500 with the recycle stream 280, i.e., as part of the second reactor feed, to hydrocracking in the second reactor 290.

[0087] Figure 2 schematically shows a process according to another exemplary embodiment for producing the present gasoline fuel component. In Figure 2, the oxygenated hydrocarbon feed 110 is supplied to the HDO reactor 120, where it is subjected to hydrodeoxygenation in the presence of the HDO catalyst 130 to obtain a hydrodeoxygenation effluent (HDO effluent) 140. The obtained HDO effluent 140 is subjected to gas-liquid separation 150 to separate a compound 160 that is gaseous at least at NTP from the HDO effluent, obtaining a degassed HDO effluent 170, which, in this exemplary embodiment, is the paraffinic hydrocarbon feed defined herein. The degassed HDO effluent 170 is then supplied in Figure 2 to the first reactor 180, where the degassed HDO effluent 170 is subjected to hydroisomerization in the presence of the hydroisomerization catalyst 190 to obtain a hydroisomerization effluent (HI effluent) 200. The obtained HI effluent 200 is subjected in Figure 2 to gas-liquid separation 210 to separate a compound 220 that is gaseous at least at NTP from the HI effluent 200, obtaining a degassed HI effluent 230. In Figure 2, the degassed HI effluent 230 is supplied to the second reactor 290, where it is subjected to hydrocracking in the presence of the hydrocracking catalyst 300 to obtain a hydrocracking effluent 350. The hydrocracking effluent 350 is subjected in Figure 2 to gas-liquid separation 360 to separate a compound 370 that is gaseous at least at NTP from the hydrocracking effluent 350, obtaining a degassed hydrocracking effluent 380. In Figure 2, the second reaction section feed containing the degassed hydrocracking effluent 380 is supplied to a distillation unit 240 that can include a single column or a pre-fractionation and a main distillation column, from which several streams or cuts can be obtained. From the distillation in Figure 2, the gasoline fuel component 390, as well as the aviation fuel component 400 and / or the diesel fuel component 410 are recovered. Further, a recycle stream 420 having a T5 boiling point of preferably 270 °C or higher can be separated. In Figure 2, the recycle stream 420 can be supplied to the second reactor 290 for hydrocracking as a co-feed with at least a portion of the degassed HI effluent 230, i.e., as a part of the second reaction section feed.In certain embodiments, yet another portion of the HI effluent 200 or 230 may be fed to the fractionation as a co-feed 500 with the hydrocracked effluent 350 or 380.

Example

[0088] Example 1 - Production of the present gasoline fuel component The gasoline fuel components studied herein were recovered from the test runs. Here, two different types of fatty raw materials were subjected to hydrodeoxygenation (HDO) and gas-liquid separation to obtain a paraffinic hydrocarbon feedstock containing >95 wt-% paraffins of the total weight of the paraffinic hydrocarbon feedstock. The paraffinic hydrocarbon feedstock was further subjected to different degrees of hydroisomerization (HI) to obtain three different hydrocracked (HC) feedstocks (feedstocks A, B, and C). Fractions of the hydroisomerization effluent obtained by degassing the hydroisomerization effluent or by recovering only the bottom fraction of the hydroisomerization effluent were hydrocracked, and subsequently the effluent from the hydrocracking was degassed. Renewable aviation fuel components were recovered as the main product from the hydrocracked effluent thus obtained, and at least gasoline fuel components were recovered as further products of particular interest here. For one of the hydrocracked effluents (test run 8), a second fraction was carried out in a manner optimized to increase the aviation fuel component yield (test run 8 using the optimized fraction, TR8o). The details of the hydrocracked feedstocks are shown in Table 1, and Table 2 shows the details of the hydrocracking process as well as the approximate boiling range and yield of the gasoline fuel components.

[0089]

Table 1

[0090] In Table 1, nP represents n-paraffin, iP represents i-paraffin, and multi-branched iP represents multi-branched i-paraffin.

[0091]

Table 2

[0092] The hydrocracking catalyst was a non-sulfided binary functional hydrocracking catalyst containing Pt on a zeolite / zeolite type material in all test runs. When the feeds reported in Table 1 were subjected to the hydrocracking conditions reported in Table 2, the catalyst had not only cracking activity but also isomerization activity.

[0093] Gasoline fuel components were produced in good yields, and generally the yields were higher at higher hydrocracking temperatures, lower WHSV, and / or higher end points such as T95 or FBP.

[0094] Example 2 - Chemical Composition and Distillation Characteristics of the Base Gasoline Fuel Component The gasoline fuel components G1 to G7 recovered in Example 1 were evaluated based on their hydrocarbon composition (Tables 3 and 4) and distillation characteristics (Table 5). The comparison was made with a conventional paraffinic gasoline component (reference gasoline, RG) obtained by subjecting the fatty raw material to HDO, moderate HI, degassing, and fractionation, i.e., without subjecting it to hydrocracking. The hydrocarbon composition analysis was performed using a detailed hydrocarbon analysis including individual component identification (for hydrocarbon groups [i-paraffin, n-paraffin, naphthene, aromatic, olefin] and carbon number [C#]). Examples of the analyzed volume fractions are shown in Tables 3 and 4. The method used was an in-house method adapted from the standard methods ASTM D6729 and EN ISO 22854.

[0095] In addition to the volume fractions of i- and n-paraffins and multi-branched i-paraffins, further characteristics such as the i- to n-paraffin ratio and average carbon number of C4 - C9 i- and n-paraffins were calculated (Tables 3 and 4). The average carbon number C of i- and n-paraffins in the C4 - C9 range avg was calculated by multiplying the volume fraction C#vol of each carbon number and further distinguishing based on hydrocarbon groups (i-paraffin, n-paraffin). From these, the average carbon numbers of i- and n-paraffins in the C4 - C9 range were calculated using the following formula.

[0096]

Number

[0097] As an example of the above calculation, the average carbon numbers of C4 - C9 n - paraffins of sample G7, which is 5.8, and C4 - C9 i - paraffins, which is 7.0, were calculated as follows:

[0098]

Number

[0099] Accordingly, the average carbon numbers of other samples were calculated.

[0100]

Table 3

[0101] In Table 3, the column of NOA indicates the total amount of naphthenes, olefins and aromatics, C# indicates the carbon number, C6 - 9m - iP indicates the amount of multi - branched i - paraffins in the range of C6 - C9, and the average C#C4 - 9 indicates the calculated average carbon number of n - paraffins and i - paraffins in the range of C4 - C9.

[0102]

Table 4

[0103] In Table 4, the column of NOA indicates the total amount of naphthenes, olefins and aromatics, C# indicates the carbon number, C6 - 9m - iP indicates the amount of multi - branched i - paraffins in the range of C6 - C9, and the average C#C4 - 9 indicates the calculated average carbon number of n - paraffins and isoparaffins in the range of C4 - C9.

[0104]

Table 5

[0105] From Tables 3 and 4, it can be seen that for gasoline fuel components G1 to G7, compared with paraffinic reference gasoline RG, the ratio of C8i - paraffin to C8n - paraffin is significantly higher, approximately 2 to 7 times, and at the same time, they contain a considerable amount of C8 paraffin. Similarly, for gasoline fuel components G1 to G7, compared with paraffinic reference gasoline RG, the ratio of C6 - C8i - paraffin to C6 - C8n - paraffin is significantly higher, at least 2 times, and at the same time, they mainly contain C6 - C8 paraffin. Gasoline fuel components G1 to G7 also have a medium average carbon number exceeding 6.0 units for i - paraffins in the C4 - C9 range, a low average carbon number less than 6.0 units for n - paraffins in the C4 - C9 range, and at least 0.7 units less than the respective average carbon numbers of i - paraffins in C4 - C9. The measured samples of gasoline fuel components according to the present disclosure have a high multi - branched C6 - C9i - paraffin content of >6.0%, further >10%, compared with <5.0% of reference gasoline RG, and at the same time mainly contain C4 - C9i - paraffin. Also, the amount of n - hexane is much less in the gasoline fuel components according to the present disclosure compared with reference gasoline RG. From Table 5, it can be seen that the method by which gasoline fuel compositions G1 to G7 have a relatively linear distillation behavior, which is beneficial for combustion characteristics, for example. The boiling point ranges reported in Table 5 indicate that the gasoline fuel components do not represent a narrow cut, but that most of the component volume boils over a rather wide temperature range. Therefore, the gasoline fuel components can be recovered in higher yields.

[0106] Example 3 - Octane Number of the Gasoline Fuel Component The properties listed in Tables 3 and 4 are closely related to the octane number of the gasoline fuel component. More specifically, it has been observed that the higher the degree of isomerization, the larger the amount of i - paraffin, and the lower the average carbon number of paraffins in the C4 - C9 range, the higher the octane number. A higher octane number is desired for use in gasoline fuel compositions for use as liquid transportation fuels.

[0107] Blended RON (EN ISO 5164-2014 corresponds to ASTM D2699-18) and Blended MON (EN ISO 5163-2014 corresponds to ASTM D2700-19) were determined from the paraffinic reference gasoline component RG and from three test run samples G3, G5, and G7 generated under similar conditions. The main difference among the above test run samples was the end cut point (about 100 °C, 120 °C, and 150 °C) (Table 6).

[0108] The quality of the gasoline fuel component was found to be affected by at least the process parameters. Higher temperature and lower WHSV in hydrocracking promoted higher i-paraffin content and slightly lower average carbon number in paraffins in the C4-C9 range when compared with samples having a similar distillation range. Judging from the set quality parameters, better gasoline fuel components were obtained at higher hydrocracking temperature and lower WHSV. Due to the small amount of the sample, the octane was determined from blending with a commercial gasoline component having a high i-paraffin content called the "second component". The blended octane number of the bRON sample was calculated using the following formula:

[0109]

Number

[0110] The blend RON and MON of gasoline fuel component sample G5 (120 °C cut) were 66.7 and 55.5, respectively. The corresponding values for sample G7 (150 °C cut) were 59.1 and 56.7. Sample G7 had a higher i-paraffin content and i- to n-paraffin ratio, but a higher average carbon number for both i- and n-paraffins. The average carbon number of paraffins in the C4-C9 range, especially C4-C9 n-paraffins, seemed to have a greater impact on RON than the i-paraffin content. The reference gasoline RG properties describing product quality were inferior to the test run gasoline fuel components. The measured test run gasoline fuel components (samples G3, G5, and G7) had significantly higher blend octane numbers than the reference gasoline RG (bRON = 46.8 and bMON = 45.3) determined from a similar blend using the same method.

[0111] Comparing the bRON and bMON results of samples derived from hydrocracked feeds B and C reveals the influence of the properties of the hydrocracked feeds (reported in Table 1) and the chemical composition of the gasoline fuel components (reported in Tables 3 and 4) on the quality of the gasoline fuel components with respect to the octane number (reported in Table 6). The most promising gasoline fuel component (G3) derived from hydrocracked feed B was compared with two gasoline fuel components (G5 and G7) derived from hydrocracked feed C. These gasoline fuel component samples were obtained from similar process conditions (with slight variations in hydrocracking temperature). The paraffin content was very similar among the samples despite different end cut points of the gasoline fuel components. The C4-C9 i-paraffin content was in the range of 68-71 vol-% and the n-paraffin was 26-29 vol-%. The relative multi-branched i-paraffin content increased as the end cut point of the gasoline fuel component sample increased, suggesting that longer paraffins underwent a higher degree of isomerization in the process. When compared again with the same paraffinic reference gasoline RG, this had a lower C4-C9 i-paraffin content of about 49 vol-% and a higher n-paraffin content of about 42 vol-%.

[0112]

Table 6

[0113] The difference in RON can be partially explained by evaluating the carbon number distribution (Tables 3 and 4). However, the analyzed samples G3, G5, and G7 have similar low C4 - C9 n - paraffin average carbon numbers (5.7 - 5.9), but there is more variation in the C4 - C9 i - paraffin average carbon numbers (6.6 - 7.0). The reference gasoline fuel component RG has a similar C4 - C9 i - paraffin average carbon number as G3, G5, and G7, but a much higher C4 - C9 range n - paraffin average carbon number (6.3). As described above, the RON value increases with the degree of isomerization and lower carbon numbers (shorter carbon chain lengths). Thus, one important differentiating factor between the octane value of the gasoline fuel components according to the present disclosure and that of the reference gasoline fuel components was the average n - paraffin carbon number in the C4 - C9 range. The G3 gasoline fuel component and the G7 gasoline fuel component have similar blend octane values, but the average i - paraffin carbon number in the C4 - C9 range is lower in the G3 gasoline fuel component, which balanced out the lower C4 - C9 range average n - paraffin carbon number of the G7 gasoline fuel component. The C4 content is relatively high in the G5 and G7 gasoline fuel components and significantly contributed to the average carbon number of the n - paraffins in the C4 - C9 range and the measured octane value. Based on the available information, the amount of C4 compounds cannot be considered to be due to the hydrocracking feedstock used because it was affected by, for example, different degassing and / or distillation procedures used to obtain the product, which could have caused differences from the selected IBP.

[0114] Based on the hydrocracking test runs using different feeds, it can be said that the feeds have some impact on the gasoline fuel component quality. Gasoline fuel components obtained by a process involving hydrocracking of paraffin streams with a high degree of isomerization have, in particular, a much better octane number than paraffinic reference gasoline components. Overall, the test runs showed that lower WHSV and / or higher temperatures in hydrocracking can improve the gasoline fuel component yield and reduce the influence of the hydrocracking feed, thereby improving the characteristics for gasoline fuel applications. On the other hand, it was shown that lower distillation endpoints (e.g., T90, T95, and / or FBP) and lower average carbon numbers of paraffins in the C4 - C9 range, especially n - paraffins in the C4 - C9 range, can improve the octane number.

[0115] Various embodiments are presented. It should be understood that in this specification, the terms comprising, including, and containing are each used as open - ended expressions without intended exclusivity.

[0116] The foregoing description has provided a complete and useful explanation of the best mode currently contemplated by the inventors for carrying out the invention as non - limiting examples of specific embodiments and implementations. However, it is clear to those skilled in the art that the invention is not limited to the details of the embodiments presented above, and can be implemented in other embodiments or different combinations of embodiments using equivalent means without departing from the features of the invention. Furthermore, some of the features of the exemplary embodiments disclosed above can be advantageously used without correspondingly using other features. Therefore, the foregoing description should be considered only as an illustration of the principles of the invention and not as limiting the invention. Accordingly, the scope of the invention is limited only by the appended claims.

Claims

1. A gasoline fuel component comprising n-paraffin, mono-branched i-paraffin, and multi-branched i-paraffin, wherein the total amount of C4-C9 n-paraffin, C4-C9 mono-branched i-paraffin, and C4-C9 multi-branched i-paraffin is more than 90 wt-% of the total weight of the gasoline fuel component, and the weight ratio of C8 i-paraffin to C8 n-paraffin is at least 4.0, preferably at least 4.5, more preferably at least 5.0, still more preferably at least 5.5, even more preferably at least 6.

0. Optionally, the total amount of C8 n-paraffin and C8 i-paraffin is at least 1.0 wt-%, preferably at least 2.5 wt-%, more preferably at least 5.0 wt-%, still more preferably at least 5.5 wt-%, even more preferably at least 6.0 wt-%, and most preferably at least 7.0 wt-% of the total weight of the gasoline fuel component. A gasoline fuel component.

2. The gasoline fuel component according to claim 1, wherein the gasoline fuel component contains at least 0.1 wt-%, preferably at least 0.3 wt-%, more preferably at least 0.5 wt-%, even more preferably at least 0.6 wt-% of C8 n-paraffin, and / or the ratio of C8 i-paraffin to C8 n-paraffin is at most 70, preferably at most 60, more preferably at most 50, still more preferably at most 40, even more preferably at most 30.

3. The gasoline fuel component according to claim 1 or 2, wherein the gasoline fuel component contains at least C6, C7, and C8 paraffins, and the weight ratio of C6-C8 i-paraffin to C6-C8 n-paraffin is at least 2.7, preferably at least 2.8, more preferably at least 3.

0. Optionally, the total amount of C6-C8 n-paraffin and C6-C8 i-paraffin is at least 50 wt-%, preferably at least 55 wt-%, more preferably at least 58 wt-% of the total weight of the gasoline fuel component.

4. The gasoline fuel component according to any one of claims 1 to 3, wherein the weight ratio of C6-C9 multi-branched i-paraffin to C6-C9 n-paraffin is at least 0.2, preferably at least 0.3, more preferably at least 0.4, even more preferably at least 0.

5.

5. The gasoline fuel component contains at least 50 wt-%, preferably at least 55 wt-%, more preferably at least 60 wt-%, even more preferably at least 65 wt-% of C4-C9 i-paraffins, and / or at least 5 wt-%, preferably at least 6 wt-%, more preferably at least 7 wt-%, even more preferably at least 10 wt-% or at least 11 wt-% of C6-C9 multi-branched i-paraffins based on the total weight of the gasoline fuel component. The gasoline fuel component according to any one of claims 1 to 4.

6. The total amount of C4-C9 n-paraffins, C4-C9 mono-branched i-paraffins and C4-C9 multi-branched i-paraffins is more than 93 wt-%, preferably more than 95 wt-% of the total weight of the gasoline fuel component, more preferably in the range of 95-99 wt-%. The gasoline fuel component according to any one of claims 1 to 5.

7. The bRON of the gasoline fuel component is determined according to ASTM D2699-18 and is at least 51, preferably at least 55, and / or the bMON of the gasoline fuel component is determined according to ASTM D2700-19 and is at least 48, preferably at least 50, more preferably at least 55. The gasoline fuel component according to any one of claims 1 to 6.

8. The average carbon number of C4-C9 i-paraffins is more than 6.0, preferably at least 6.2, more preferably in the range of 6.2-8.0, and / or the average carbon number of C4-C9 n-paraffins is at most 6.0, preferably at most 5.6, preferably at least 0.5 units lower, more preferably at least 0.6 units lower than the average carbon number of C4-C9 i-paraffins. The gasoline fuel component according to any one of claims 1 to 7.

9. The C6n-paraffin content is at most 11 wt-%, preferably at most 8 wt-% of the total weight of the gasoline fuel component, and / or the weight ratio of C6i-paraffin to C6n-paraffin is at least 1.5, preferably at least 1.

7. The gasoline fuel component according to any one of claims 1 to 8.

10. The bio-based carbon content of the gasoline fuel component is determined according to EN 16640 (2017) and is at least 50 wt-% based on the total weight (TC) of carbon in the gasoline fuel component, preferably at least 70 wt-%, more preferably at least 90 wt-%, even more preferably at least 95 wt-%, and even more preferably about 100 wt-%, the gasoline fuel component according to any one of claims 1 to 9.

11. The difference between the T90 temperature (90 vol-% recovery determined according to ASTM D7096-19) and the T10 temperature (10 vol-% recovery determined according to ASTM D7096-19) is within the range of 60 to 140 °C, such as at least 60 °C, more preferably at least 70 °C, even more preferably at least 80 °C or at least 100 °C, the gasoline fuel component according to any one of claims 1 to 10.

12. Hydrodeoxygenation of an oxygenated hydrocarbon feedstock typically containing vegetable oil, animal fat and / or microbial oil, and preferably obtaining a paraffinic hydrocarbon feedstock, optionally followed by gas-liquid separation and / or fractionation of the paraffinic feedstock fraction, subjecting the paraffinic hydrocarbon feedstock to at least hydroisomerization, preferably to hydroisomerization and hydrocracking, followed by fractionation, and recovering at least the gasoline fuel component from the fraction, The gasoline fuel component according to any one of claims 1 to 11, which can be obtained by a process comprising.

13. Providing a paraffinic hydrocarbon feedstock containing at least 60 wt-% of paraffin based on the total weight of the paraffinic hydrocarbon feedstock, with a maximum of 30 wt-% of the paraffin in the paraffinic hydrocarbon feedstock being i-paraffin, In a first reaction section, preferably a first reactor, subjecting the paraffinic hydrocarbon feedstock to hydroisomerization in the presence of a hydroisomerization catalyst to obtain a hydroisomerization effluent, Subjecting a second reaction section feedstock containing at least a portion of the hydroisomerization effluent to hydrocracking in the presence of a hydrocracking catalyst in a second reaction section, preferably a second reactor, to obtain a hydrocracking effluent, Subjecting the hydrocracking effluent and, optionally, a portion of the hydrogen isomerization effluent to fractionation to recover at least the gasoline fuel component and, optionally, the aviation fuel component from the fractionation, The gasoline fuel component according to any one of claims 1 to 12, which can be obtained by a process comprising.

14. Use of the gasoline fuel component according to any one of claims 1 to 13 in a gasoline fuel composition.

15. A gasoline fuel composition comprising the gasoline fuel component according to any one of claims 1 to 13.

16. The use according to claim 14, or the gasoline fuel composition according to claim 15, wherein the gasoline fuel composition comprises at least one or more of an oxygenated gasoline fuel component and / or a hydrocarbon cut, preferably ethanol, propanol, i-propanol, butanol, i-butanol, tert-butanol, pentanol, i-pentanol, MTBE, ETBE, TAME, TAEE, butane, alkylate, isomerate, raffinate, FCC gasoline, reformate, pygas and / or light straight run (LSR) gasoline.

17. The use according to claim 14 or 16, or the gasoline fuel composition according to claim 15 or 16, wherein the gasoline fuel composition meets the requirements of gasoline fuel as defined in Directive 2009 / 30 / EC and, optionally, EN 228:2012 as amended in 2017.

18. The use according to any one of claims 14, 16 or 17, or the gasoline fuel composition according to any one of claims 15, 16 or 17, wherein the gasoline fuel composition comprises the gasoline fuel component according to any one of claims 1 to 13 in an amount of 1 to 25% -vol, preferably 1 to 20% -vol, of the total volume of the gasoline fuel composition.

19. Use of the gasoline fuel component according to any one of claims 1 to 13 in raw materials for industrial conversion processes, preferably in pyrolysis raw materials and / or catalytic cracking raw materials, in solvents, carriers, dispersant compositions, demulsifiers, extractants, surfactants, degreasing compositions, detergents, thinners, penetrating oils, anticorrosive compositions, multi-purpose oils, in metalworking, in agriculture, in construction, in electronic devices, in medical devices, in compositions for the automotive, electrical, textile, packaging, paper and / or pharmaceutical industries, and / or in the manufacture of intermediates therefor.

20. Use according to any one of claims 14, 16, 17, 18 or 19, the gasoline fuel composition according to any one of claims 15 to 18, or the gasoline fuel component according to any one of claims 1 to 13, wherein at least one or more of an antioxidant, a stabilizer, a surfactant, a corrosion inhibitor, a friction modifier, a metal deactivator, and / or a fuel dye are added to the gasoline fuel component or the gasoline fuel composition.

Images