Renewable base components of high performance renewable gasoline and integrated process for their preparation

Abstract

A high-octane renewable base gasoline composed of a reformate renewable base component and an isomerate base component is described, wherein said base gasoline is present in a high octane fully renewable gasoline fuel composition.

Description

[0001] RENEWABLE BASE COMPONENTS OF HIGH PERFORMANCE RENEWABLE

[0002] GASOLINE AND INTEGRATED PROCESS FOR THEIR PREPARATION

[0003] The present invention relates to renewable base components of fully renewable high performance gasoline, in particular high octane performance gasoline.

[0004] The present invention also relates to the integrated process for the preparation of said renewable base components from renewable feedstocks such as, for example, vegetable oils .

[0005] In this description, the term "renewable" will be used as a synonym for the term "of renewable origin" , "from renewable biofuel sources" and is intended to identify products of renewable origin or products resulting from the processing of biofuel from renewable origin such as, for example, vegetable oils.

[0006] In the automotive sector, there is an increasing demand for fuels of completely renewable origin, not only diesel cuts, also referred to here as diesel fuels, but also gasoline cuts, also referred to here as gasoline fuels.

[0007] As far as diesel fuels of completely renewable origin are concerned, there are a number of industrially established processes for obtaining diesel cuts from renewable sources, including the process known as Ecofining™. This process that has been developed to obtain a hydrogenated vegetable oil (HVO) usable as a diesel fuel, also produces a naphtha cut fraction, in smaller quantities, that is currently not used in fuel formulation.

[0008] As far as gasoline fuels that can be defined as "from renewable origin", efforts to date have mainly focused on

[0009] - obtaining ethanol and / or other oxygenated gasoline components of renewable origin such as ethers or other alcohols (ETBE, MTBE, butanol) , to be added to mineral gasoline in quantities that comply with EN 228, e.g. 5% vol / vol (E5) or 10% vol / vol (E10) ; and / or

[0010] - identifying the appropriate blending percentage of a gasoline component of renewable origin, e.g. 15% vol max, with a gasoline component of fossil origin and oxygenated components. In fact, one of the problems in obtaining renewable gasoline by adding a percentage of renewable gasoline component is being able to achieve the minimum RON of 95 (required by the EN228 specification) , since the renewable gasoline component currently has a low aromatic content, which is much lower than the mineral component, resulting in RON values much lower than 95.

[0011] There are also gasoline fuels of completely renewable origin that comply with EN228 in terms of RON and contain oxygenated components, possibly of renewable origin.

[0012] However, the addition of such oxygenated components, even if of renewable origin, decreases the heat generated by gasoline per unit volume in use.

[0013] It would therefore be desirable to have at least one renewable base component of gasoline with a high octane number, e.g. having a RON of at least 95, preferably of at least 100, and consequently to be able to have a gasoline fuel of renewable origin having a RON of at least 95, preferably of at least 100, without having to use oxygenated compounds to achieve this minimum RON value.

[0014] In particular, it would be desirable to have renewably sourced base gasoline components apt for use in blending to obtain a gasoline fuel with a RON of at least 95, and with chemical-physical and engine-related characteristics aligned to fossil counterparts, while using a naphtha cut of renewable origin derived from the production of renewable diesel in order to get the most of the renewable feedstock in the production of automotive fuels.

[0015] It is therefore a first object of the present invention a renewable base fuel component of a gasoline fuel characterized by being a reformed (reformate) renewable component, generally a catalytic reformed component, having a RON of at least 95, preferably ranging from 95 to 105, more preferably having a RON of at least 100, said reformate renewable base component being a mixture of hydrocarbons comprising aromatic hydrocarbons, naphthenes (i.e. saturated cyclic hydrocarbons) , linear paraffins, isoparaffins, wherein the iso-paraffin content is equal to, or greater than, 10% by weight, preferably greater than 16% by weight, with respect to the weight of the total hydrocarbons.

[0016] The RON of this reformate renewable base component is generally measured according to ISO 5164.

[0017] Said reformate renewable base component also advantageously exhibits

[0018] - an initial boiling point (I.B.P) which can range from 30°C to 50°C, preferably from 35°C to 48°C;

[0019] - a final boiling point (F.B.P. ) which can range from 190°C to 220°C, preferably 193°C to 220°C;

[0020] - a boiling point T10 %vol which can range from 60°C to 90°C, preferably from 63°C to 78°C;

[0021] - a boiling point T20 %vol which can range from 80°C to 105°C, preferably from 80°C to 103°C;

[0022] - a boiling point T90% vol which can range from 150°C to 170°C, preferably 153°C to 163°C.

[0023] The term "fuel base component of a gasoline fuel" here is intended to mean one or more combustible hydrocarbon compounds suitable for combustion in an endothermic engine, which must be present in the final gasoline fuel formulation to meet certain requirements and / or regulations of fuels, e.g. gasoline, which are available at the fuel pump (i.e. ready-to-use) .

[0024] The term "reformate hydrocarbon component (R) " here is intended to mean a hydrocarbon mixture obtained by catalytic reforming, as will be detailed below.

[0025] Said reformate renewable component also shows:

[0026] - a boiling point T30%vol ranging from 97°C to 117°C;

[0027] - a boiling point T70% vol ranging from 128°C to 142°C;

[0028] - a boiling point T80% vol ranging from 140°C to 150°C.

[0029] The aforesaid ranges and boiling points can be determined according to any of the techniques known in the art, for example according to ISO 3405 or ASTM D86, preferably ISO 3405, without thereby departing from the scope of the present invention .

[0030] Said reformate renewable base component is a mixture of hydrocarbons having a number of carbon atoms generally ranging from 5 to 11 and comprises aromatic hydrocarbons, naphthenes (i.e. , saturated cyclic hydrocarbons) , linear paraffins, iso-paraffins: among the aromatics present, a predominance of aromatics with a number of carbon atoms ranging from 7 to 9 (C7, C8, C9) and, among the paraffins present, a predominance of paraffins with a number of carbon atoms ranging from 5 to 7 (C5, C6 and C7) were observed. Said reformate renewable hydrocarbon component R may or may not contain benzene, preferably it does not contain benzene: if present, its concentration is less than 2% by weight, preferably less than 1.5% by weight with respect to the weight of the total hydrocarbons.

[0031] Said reformate renewable base component R shows an aromatic content (excluding benzene) of at least 60% by weight with respect to the total weight of the hydrocarbons, which can be up to 80% by weight, preferably 65% by weight to 75% by weight, more preferably 70-75% by weight.

[0032] The aromatics and benzene content may be measured according to one of the methodologies known in the art, for example according to ASTM D6839, according to ASTM D6730 or according to EN 22854, preferably according to ASTM D6730, without thereby departing from the scope of the present invention .

[0033] Among the aromatics present in said reformate renewable base component, the predominance of aromatics with a number of carbon atoms from 7 to 9 (C7, C8, C9) was observed, in particular the predominance of C7 and C8.

[0034] Said reformate renewable base component R shows a total saturated hydrocarbon content ranging from 15% by weight to 40% by weight, more preferably from 18% by weight to 36% by weight, more preferably from 25% by weight to 35% by weight, with respect to the weight of the total hydrocarbons. In one embodiment of the invention, the content of saturated hydrocarbons in said renewable reformate component is equal to or higher than 25% by weight up to 40% by weight.

[0035] The determination of the saturated hydrocarbon content can be performed by any of the methods known in the art, preferably according to ISO 22854.

[0036] In particular, said reformate renewable base component R has an n-paraffin content ranging from 5% to 10% by weight with respect to the total weight of the total hydrocarbons.

[0037] The content of said n-paraffins can be determined according to any of the methods known in the art without thereby departing from the scope of the present invention, preferably according to ASTM 6730.

[0038] Said reformate renewable base component R exhibits an iso-paraffin content ranging from 10% by weight to 35% by weight, preferably from 15% by weight to 25% by weight, more preferably greater than 18% by weight, with respect to the weight of the total hydrocarbons.

[0039] The content of iso-paraffins can be determined by the same methods used for n-paraffins, preferably according to ASTM D6730, without thereby departing from the scope of the present invention.

[0040] In this reformate renewable base component, olefins may also be present in quantities advantageously less than 3%, which can range from 0.70 to 2% by weight, preferably 0.8% to 1.5% by weight, with respect to the weight of the total hydrocarbons .

[0041] The olefin content may be measured according to methodologies known in the art, for example according to ASTM D6839 or according to ASTM D6730, preferably ASTM D6730, without thereby departing from the scope of the present invention .

[0042] Said reformate renewable base component R generally has a density in the range from 770 kg / m3to 825 kg / m3, preferably from 780 kg / m3to 825 kg / m3.

[0043] Said reformate renewable base component R exhibits a lower heating value (LHV) ranging from 41 to 46 MJ / kg, preferably from 41 to 43 MJ / kg.

[0044] An example of a reformate renewable base component R (referred to in Table 1 as "BIO reformate" for simplicity) having a RON of at least 95 according to the invention may be the reformate having the characteristics shown in Table 1 (in comparison with those of a reformate mineral base gasoline component referred to in the table as "fossil reformate" for simplicity) .

[0045] Table 1: characteristics BIO reformate vs. fossil reformate

[0046] The reformed renewable base component R of the present invention is derived from the catalytic reforming of a "heavy" renewable naphtha with a high isoparaffin content, hereafter referred to as HVO-HVN (Heavy Naphtha) for simplicity. Catalytic reforming is a generally known catalytic process in the art of fossil fuels and will be described in detail below.

[0047] The "heavy" renewable naphtha HVO-HVN (also referred to herein as "100°+ naphtha") from which the reformate renewable base component described above is derived is a hydrocarbon mixture in which the number of carbon atoms of said hydrocarbons is predominantly greater than 6 up to 12, preferably 7 to 9.

[0048] Said renewable heavy naphtha does not contain benzene.

[0049] The hydrocarbon mixture that makes up the aforesaid heavy renewable naphtha comprises aromatic hydrocarbons, naphthenes, linear paraffins and iso-paraffins.

[0050] In said heavy renewable naphtha, the following was observed :

[0051] - among the aromatics, a predominance of aromatics having a number of carbon atoms from 7 to 9 (C7, C8, C9) ;

[0052] - among the paraffins, a predominance of paraffins having a number of carbon atoms from 7 to 9.

[0053] Said heavy renewable naphtha HVO-HVN exhibits:

[0054] - an I.B.P ranging from 95°C to 105°C, preferably from 99°C to 102°C;

[0055] - an F.B.P ranging from 190°C to 200°C, preferably from

[0056] 193°C to 196°C. Said heavy renewable naphtha HVO-HVN exhibits:

[0057] - a boiling point 110% vol / vol ranging from 105°C to 110°C, preferably from 105°C to 108°C;

[0058] - a boiling point 190% vol / vol ranging from 140°C to 150°C, preferably from 140°C to 145°C.

[0059] In addition, said heavy renewable naphtha HVO-HVN exhibits :

[0060] - a boiling point 120% vol / vol ranging from 106°C to 115°C, preferably from 107°C to 110°C;

[0061] - a boiling point 150% vol / vol ranging from 110°C to 120°C, preferably from 113°C to 117°C.

[0062] Ihe aforesaid boiling ranges and boiling points can be determined according to ISO 3405 or AS1M D86, preferably ISO 3405, without thereby departing from the scope of the present invention .

[0063] Said heavy renewable naphtha HVO-HVN also has a density in the range of 700 to 735 kg / m3, preferably 700 to 725 kg / m3.

[0064] Said heavy renewable naphtha HVO-HVN exhibits an aromatic content of less than 5% by weight with respect to the weight of the total hydrocarbons.

[0065] In an embodiment, the aromatic content in said heavy renewable naphtha HVO-HVN ranges from 0.1% by weight to 4% by weight with respect to the weight of the total hydrocarbons, preferably from 0.1% by weight to 3.5% by weight, more preferably from 0.5% by weight to 3.0% by weight, even more preferably from 0.5% by weight to 1.5% by weight, said values being lower with respect to the aromatic content in a similar heavy naphtha of mineral origin.

[0066] The aromatic content (excluding benzene) in the heavy renewable naphtha can be measured according to any one of the methodologies known in the art, for example according to EN 22854, according to ASTM D6839 or according to ASTM D6730, preferably according to ASTM D6730, without thereby departing from the scope of the present invention.

[0067] Furthermore, said heavy renewable naphtha HVO-HVN exhibits an isoparaffin content of at least, or even more than, 35% by weight with respect to the weight of the total hydrocarbons, which may be as high as 75% by weight, preferably 40 to 70% by weight, more preferably 40% to 65% by weight, without thereby departing from the scope of the present invention.

[0068] These values are higher than the isoparaffin content in a similar heavy naphtha of mineral origin.

[0069] The content of n-paraffins and iso-paraffins in said heavy renewable naphtha HVO-HVN can be measured according to one of the methodologies known in the art and disclosed above for the reformate, preferably according to ASTM D6730, without thereby departing from the scope of the present invention . In addition, said heavy renewable naphtha HVO-HVN contains naphthenes in amounts of less than 30% by weight with respect to the weight of the total hydrocarbons, preferably 1 to 15% by weight, more preferably 10 to 15% by weight, which are much lower values than the naphthene content in a heavy naphtha of mineral origin.

[0070] The aforesaid naphthenic content can be measured according to methodologies known in the art, for example in accordance with ASTM D6730, without thereby departing from the scope of the present invention.

[0071] In a preferred embodiment, the heavy renewable naphtha, which is the precursor of the reformate base component, exhibits (according to ASTM D6730) :

[0072] - an aromatic content ranging from 0.5% to 3% by weight;

[0073] - an isoparaffin content ranging from 40% by weight to 70% by weight, preferably from 40% by weight to 65% by weight .

[0074] Said preferred heavy renewable naphtha can also have a naphthene content ranging from 5% to 20% by weight.

[0075] An example of such a heavy renewable naphtha HVO-HVN in accordance with the invention is that having the characteristics shown in Table 2 below compared with those of a heavy naphtha of mineral origin (referred to in the table as HVN (FOSSIL) for simplicity) . Table 2: Characteristics of Heavy Naphtha obtained by

[0076] Splitting

[0077] As mentioned above, said heavy renewable naphtha HVO-HVN can be produced by a splitting process of a starting renewable naphtha (hereafter also referred to as HVO

[0078] Naphtha" for simplicity) having

[0079] - an I.B.P. ranging from 25°C to 45°C, preferably 37°C to 42°C; and

[0080] - F.B.P. ranging from 165°C to 176°C, preferably 173°C to 175°C.

[0081] Said I.B.P. and F.B.P. of said starting naphtha can be measured by one of the known techniques used to detect distillation temperature (atmospheric or vacuum) of mixtures of hydrocarbons, for example ASTM D2887, ISO 3405, ASTM D2287, preferably ISO 3405, without thereby departing from the scope of the present invention.

[0082] The starting renewable naphtha (HVO Naphtha) , from which HVO-HVN heavy renewable naphtha according to the invention may be derived, is a renewable hydrocarbon mixture of naphthenic, n-paraffin and iso-paraffin hydrocarbons having a low aromatic content compared to a mineral naphtha, where said hydrocarbons generally have a number of carbon atoms ranging from 4 to 12.

[0083] Said starting renewable naphtha (HVO Naphtha) contains olefins in negligible quantities (less than 0.1% by weight with respect to the weight of the total hydrocarbons) and has an aromatic hydrocarbon content (excluding benzene) of less than 5% by weight with respect to the weight of the total hydrocarbons, generally a content of 1% by weight to 2% by weight .

[0084] The content of aromatics in the starting renewable naphtha (HVO Naphtha) can be measured according to one of the methodologies known in the art, for example according to ASTM D6839, according to ASTM D6730 or according to EN 22854, preferably according to ASTM D6730, without thereby departing from the scope of the present invention.

[0085] Said starting renewable naphtha (HVO Naphtha) exhibits a high content of saturated hydrocarbons, which can range from 90% by weight to 99% by weight with respect to the weight of the total hydrocarbons.

[0086] In particular, said starting renewable naphtha (HVO Naphtha) exhibits a linear paraffinic hydrocarbon content substantially similar to fossil naphtha, e.g. 28% by weight with respect to the weight of the total hydrocarbons.

[0087] Said starting renewable naphtha (HVO Naphtha) is characterized by a high isoparaffin content, generally higher than that of fossil naphtha.

[0088] Said starting renewable naphtha (HVO Naphtha) exhibits in particular a content of iso-paraffinic hydrocarbons substantially similar to heavy renewable naphtha HVO-HVN, of at least, or even more than, 35% by weight with respect to the weight of the total hydrocarbons, which may be up to 75% by weight, more preferably from 40% by weight to 70% by weight, more preferably from 40% by weight to 65% by weight, without thereby departing from the scope of the present invention .

[0089] The aforesaid n-paraffin and iso-paraffin content can be measured according to methodologies known in the art, for example according to ASTM D6839 or preferably according to ASTM D6730, without thereby departing from the scope of the present invention.

[0090] In addition, said starting renewable naphtha (HVO Naphtha) surprisingly contains naphthenes, albeit in a lower concentration than a fossil naphtha: this was unexpected as it was expected the absence of naphthenes given that the starting renewable naphtha is derived (as will be explained in detail below) from an isomerization reaction that is known to transform cyclic alkanes (naphthenes) and linear alkanes into branched alkanes.

[0091] Generally, the naphthene content in said starting renewable naphtha (HVO Naphtha) is less than 20% by weight with respect to the weight of the total hydrocarbons, preferably from 1% by weight to 15% by weight, more preferably from 3% by weight to 10% by weight, which is far lower than that of a similar naphtha of fossil origin.

[0092] The aforesaid naphthenic content can be measured according to methodologies known in the art, for example in accordance with ASTM D6730, without thereby departing from the scope of the present invention.

[0093] Said starting renewable naphtha (HVO Naphtha) contains olefins in negligible quantities (less than 0.1% by weight with respect to the weight of the total hydrocarbons) and has an aromatic hydrocarbon content of less than 5% by weight with respect to the weight of the total hydrocarbons, generally a content of 1% by weight to 2% by weight.

[0094] The aforesaid aromatic content in the starting renewable naphtha can be measured according to one of the methodologies known in the art, for example according to ASTM D6839, according to ASTM D6730 or according to EN 22854, preferably according to ASTM D6730, without thereby departing from the scope of the present invention.

[0095] Said starting renewable naphtha (HVO Naphtha) exhibits

[0096] - a boiling point T10 %vol which can range from 55°C to 63°C, preferably from 58°C to 61°C;

[0097] - a boiling point T90 %vol which can range from 130°C to 140°C, preferably 134°C to 137°C.

[0098] This starting renewable naphtha (HVO Naphtha) also exhibits :

[0099] - a boiling point T20 %vol which can range from 60°C to 70°C, preferably from 64°C to 68°C;

[0100] - a boiling point T30 %vol which can range from 70°C to

[0101] 80°C, preferably 73°C to 76°C; - a boiling point T50%vol which can range from 85°C to 98°C, preferably 88°C to 95°C.

[0102] The aforesaid boiling ranges can be measured according to ISO 3405, ASTM D86, ASTM D2887, preferably ISO3405, without thereby departing from the scope of the present invention .

[0103] Said starting renewable naphtha (HVO naphtha) has a RON value generally greater than 30, preferably a RON of at least 35, more preferably a RON of 40-40: generally, this type of naphtha is used in the art as a possible component among the components of gasoline.

[0104] A specific example of such a starting renewable naphtha (HVO Naphtha) is one having the characteristics shown in Table 3, e.g. a naphtha produced by the Ecofining process, as compared to a typical fossil naphtha that typically undergoes a splitting step.

[0105] Table 3: HVO Naphtha vs. Fossil Naphtha

[0106] As can be seen from Table 3, the main differences between a starting renewable Naphtha (HVO Naphtha) - which is a precursor to the reformate component of the invention having a high RON - and its fossil homologous lie in the type of hydrocarbons that are present.

[0107] The starting renewable naphtha (HVO Naphtha) has a high iso-paraffin content, a low naphthene content and virtually no aromatics . In contrast, the fossil homologous has a reduced isoparaffin content for the benefit of higher naphthenes and aromatics .

[0108] Said starting renewable naphtha (HVO Naphtha) is generally one of the products of a process of hydrotreating vegetable oils (or more generally renewable feedstocks including used cooking oils, animal fats and the like) that takes place in two catalytic stages and in the presence of hydrogen, such as the process identified as Ecofining™.

[0109] In the process of hydrotreating vegetable oils such as the Ecofining process™, the vegetable oil (or more generally the renewable feedstock mentioned above) consisting of a mixture of triglycerides and fatty acids undergoes a hydrodeoxygenation process in the first catalytic stage, from which a fully deoxygenated product is obtained consisting mainly of linear paraffinic chains with a number of carbon atoms ranging from 15 to 20 (C15-C20) .

[0110] The deoxygenated product obtained in the first stage is then subjected to isomerization in the second catalytic stage, resulting in a hydrotreated vegetable oil HVO.

[0111] This HVO product is made up of a mixture of hydrocarbons (isoparaffins, n-paraffins, naphthenes) which undergo a fractionation process to obtain other lighter cuts such as

[0112] HVO-Naphtha, HVO- JET in addition to HVO-DIESEL. An example of such an Ecofining process™ is that described in the patents and / or patent applications EP2084245B1 W02008113492 , EP2134817A1, W02015 / 181744 , W02020053118A1 incorporated herein in full by reference.

[0113] In this Ecofining process, the feedstock of renewable origin, possibly pre-treated with processes to decrease the phosphorus and metal salt content, undergoes the catalytic hydrodeoxygenation reaction using, as a catalyst, mixed cobalt and molybdenum sulphides, or Ni-Mo, Ni-W, Co-W, supported on alumina: the aforesaid catalytic hydrodeoxygenation step can be conducted with hydrogen, at a pressure ranging between 25 bar and 70 bar, preferably between 30 bar and 50 bar; the temperature of the catalytic hydrodeoxygenation step can be comprised between 240°C and 450°C, preferably between 270°C and 430°C.

[0114] Preferably operation takes place with a liquid hourly space velocity (LHSV) which can range from 0.5 hours™ to 2 hours™, more preferably from 0.5 hours™ to 1 hour™ . The fb / feedstock ratio should preferably be comprised between 400 and 2000 Nl / 1.

[0115] Subsequently, in the second step of the Ecofining process, the mixture containing the linear alkanes obtained from the aforesaid hydrodeoxygenation reaction is subjected to hydroisomerization, in the presence of hydrogen, using a solid acid catalyst, thus obtaining a mixture containing branched alkanes.

[0116] An example of a solid acid catalyst that can be used in the hydroisomerization step is a catalytic system comprising a metal component containing one or more group VIII metals, possibly in a mixture with one or more group VIB metals, and a carrier of an acidic nature comprising a fully amorphous micro-mesoporous silico-alumina, preferably having a SiO2 / A12Oa molar ratio comprised between 30 and 500, a surface area greater than 500 m2 / g, a pore volume comprised between 0.3 and 1.3 ml / g, an average pore diameter of less than 40 Angstrom, e.g. Pt / MSA, as described in patent application EP2134817A1 incorporated herein in its entirety as a reference .

[0117] The aforesaid hydroisomerization step can be conducted at a temperature comprised between 250°C and 450°C, preferably between 280°C and 380°C; the operating pressure of said hydroisomerization step can be comprised between 25 bar and 70 bar, preferably between 30 bar and 50 bar. Preferably operation takes place with an LHSV ranging from 0.5 hours-1to 2 hours-1. The H2 / HC ratio should preferably be comprised between 200 and 1000 Nl / 1.

[0118] As mentioned above, this starting renewable naphtha ( H VO -Naphtha ) , e.g. derived from the Ecofining process™, is subjected to splitting producing not only a heavy renewable naphtha HVO-HVN as described above, but also a "light" renewable naphtha , hereafter also referred to as HVO-LVN for simplicity .

[0119] The splitting step, also referred to herein as the fractionation step or fractional distillation step, is operated in such a manner as to predominantly separate hydrocarbons having carbon numbers of 7 and higher (C7+) from hydrocarbons having carbon numbers of 6 and lower (C6 and C6-) , thus obtaining the separation of a first mixture of hydrocarbons, preferably having the characteristics of heavy naphtha as described above, from a second mixture of hydrocarbons preferably having the characteristics of light naphtha as described in detail below.

[0120] Such splitting can advantageously take place at a cut temperature (fractional distillation) ranging from 97°C to 100°C, although this is not binding for the purposes of the present invention.

[0121] Such splitting can also advantageously take place at atmospheric pressure, although this is not binding for the purposes of the present invention.

[0122] This light renewable naphtha HVO-LVN is a mixture of hydrocarbons having carbon numbers generally ranging from 3 to 7, with a large proportion of hydrocarbons having carbon numbers of 6 and below (C6 and C6-) , in the form of n- paraffinic, iso-paraffinic, naphthenic, aromatic, and olefinic hydrocarbons (negligible amounts, less than 0.1% by weight with respect to the weight of the total hydrocarbons) .

[0123] This light renewable naphtha HVO-LHV has an I.B.P. ranging from 33°C to 36°C and an F.B.P. ranging from 70°C to 73°C .

[0124] The above boiling ranges can be measured according to ISO 3405 or ASTM D86, preferably ISO 3405, without thereby departing from the scope of the present invention.

[0125] This light renewable naphtha HVO-LHV exhibits:

[0126] - a boiling point T10% vol / vol which can range from 41°C to 45°C;

[0127] - a boiling point T95% vol / vol which can range from 65°C to 68 °C .

[0128] This light renewable naphtha HVO-LHV also exhibits a boiling point T50% vol / vol which can range from 49°C to 52°C.

[0129] The aforementioned boiling points can be measured according to ISO 3405 or ASTM D86, preferably ISO 3405, without thereby departing from the scope of the present invention .

[0130] This light renewable naphtha HVO-LVN also has a density that varies in the range from 645 kg / m3to 655 kg / m3.

[0131] Said light renewable naphtha HVO-LVN exhibits a negligible aromatic content of less than 1% by weight with respect to the total weight of the hydrocarbons, generally a content ranging from 0.05% by weight to 0.5% by weight, preferably less than 0.2% by weight.

[0132] The aromatic content in the light renewable naphtha HVO- LVN can be measured according to one of the methodologies known in the art and described above, preferably according to ASTM D6730, without thereby departing from the scope of the present invention.

[0133] Said light renewable naphtha HVO-LVN exhibits an isoparaffin content greater than 40% by weight with respect to the total weight of the hydrocarbons, preferably 60% to 70% by weight, values far greater than those detectable in a light mineral naphtha from splitting containing hydrocarbons with less than 7 carbon atoms.

[0134] The iso-paraffin content of said light renewable naphtha HVO-LVN can be measured according to one of the methodologies known in the art and described above, preferably according to ASTM D6730, without thereby departing from the scope of the present invention.

[0135] In addition, said light renewable naphtha HVO-LVN shows a naphthene content of less than 10% by weight with respect to the weight of the total hydrocarbons, generally less than 5% by weight, preferably ranging from 3% by weight to 4% by weight, more preferably around 3.5%-4% by weight, which is far lower than that of a light naphtha of fossil origin. The aforesaid naphthene content can be measured according to one of the methodologies known in the art and described above, preferably ASTM D6730, without thereby departing from the scope of the present invention. This light renewable naphtha HVO-LVN also exhibits a lower heating value (LHV) which can range from 44 MJ / kg to 46 MJ / kg.

[0136] In a preferred embodiment, the light renewable naphtha HVO-LVN exhibits (according to ASTM D6730) : - an aromatic content ranging from 0.05% by weight to 0.2% by weight;

[0137] - an isoparaffin content ranging from 45% by weight to 70% by weight, preferably 60% by weight to 65% by weight;

[0138] - a naphthene content of less than 10% by weight, preferably less than 5% by weight.

[0139] An example of a light renewable naphtha HVO-LVN is one that has the characteristics shown in Table 4.

[0140] Table 4: Renewable vs. fossil light naphtha characteristics

[0141] Said light renewable naphtha HVO-LVN can advantageously be sent to an isomerization step in order to obtain a fuel isomerate base component of renewable origin for gasoline fuel, which can be used in combination with the reformate component having a high RON according to the invention to form a base gasoline and the corresponding gasoline fuel composition as will be illustrated in detail below.

[0142] The isomerate base component of renewable origin for gasoline that can be used in combination with the renewable reformate base component having a high RON according to the invention is a mixture of hydrocarbons comprising isoparaffinic, naphthenic, and linear n-paraffinic hydrocarbons, and with substantially no olefins or aromatics (excluding benzene) , said hydrocarbons having a carbon number of 4 to 7, with a predominance of C5 and C6 hydrocarbons .

[0143] The isomerate component of renewable origin for gasoline that can be used in combination with the reformate component having a high RON according to the invention advantageously exhibits an I.B.P. which can range from 32°C to 35°C and an F.B.P. which can range from 73°C to 78°C.

[0144] The above boiling points can be measured according to ISO 3405 or ASTM D86, preferably ISO 3405, without thereby departing from the scope of the present invention

[0145] Said isomerate renewable component also exhibits a boiling point T10 %vol which can range from 38°C to 42°C, preferably 39°C to 42°C.

[0146] Said isomerate renewable component exhibits a boiling point T90% vol which can range from 58°C to 62°C.

[0147] Said renewable isomerate component also exhibits:

[0148] - a boiling point T60 %vol which can range from 43°C to 49°C;

[0149] - a boiling point T70 %vol which can range from 47°C to

[0150] 53°C; a boiling point T95% vol which can range from 57°C to

[0151] 65°C.

[0152] The aforesaid renewable isomerate base component also exhibits

[0153] - a boiling point T30 %vol which can range from 40°C to 44°C;

[0154] - a boiling point T50 %vol which can range from 44°C to 48°C;

[0155] - a boiling point T80% vol which can range from 49°C to 56°C.

[0156] The aforementioned boiling points can be measured according to ISO 3405 or ASTM D86, preferably ISO 3405, without thereby departing from the scope of the present invention .

[0157] This renewable isomerate base component also exhibits a paraffin content (linear + branched) greater than 90% m / m, generally greater than 97% m / m.

[0158] This renewable isomerate base component also exhibits an iso-paraffin content greater than 78% by weight of total hydrocarbons, preferably greater than 80% by weight, more preferably around 85-90% by weight, which is well above that of an isomerated gasoline component of fossil origin.

[0159] The aforesaid iso-paraffin content can be measured according to one of the methodologies known in the art and disclosed above, preferably according to ASTM D6730, without thereby departing from the scope of the present invention.

[0160] This renewable isomerate base component also shows a naphthene content of less than 5% by weight with respect to the weight of the total hydrocarbons, generally around 2-3% by weight, which is far lower than that of an isomerate base component of fossil origin.

[0161] In an embodiment, the renewable isomerate base component usable in combination with the present reformate renewable base component according to the invention has the following characteristics as shown in Table 5.

[0162] Table 5:Renewable (BIO) vs. fossil isomerate characteristics

[0163] The process of isomerization of linear alkane hydrocarbons is known in the art and is generally conducted at a temperature of 240-250°C and a pressure of about 15-20 barg, in the presence of conventional isomerization catalysts that induce the formation of carbocations such as aluminium chloride or bromide, platinum or plat inum-rhenium, plat inum-germanium in combination with aluminium trichloride supported on alumina. With regard to the catalytic reforming process , it is a catalytic process that produces aromatics from precursors contained in the starting feedstock. Feedstock suitable for catalytic reforming is characterized by the presence of naphthenic and aromatic compounds. In processes for obtaining the fossil reformate base component of fossil fuels, it is typically assessed whether a reformed component with RON values above 95 is industrially obtainable (i.e. with yields greater than 60%) , e.g. 100, at the catalytic reforming operating temperatures by calculating the N+A value of the feedstock for catalytic reforming where N= [naphtheni c concentration] and A= [aromatic concentration] : the N+A value of the fossil feedstock which is considered as the minimum for reforming is 35-40 according to the catalytic reforming technical manuals. See e.g. George J. Antos, Abdullah M. Aitani "Catalytic Naphtha Reforming", Second Edition (2005) , MARCEL DEKKER, INC. , Chapter 3.3, page 15.

[0164] It was therefore unexpected that the heavy renewable naphtha described above in accordance with the invention has produced a reformate renewable base component with a RON of at least 95, in particular a RON of at least 100, despite having N+A values much lower than 35, e.g. about 15 in the case of the naphtha in Table 2.

[0165] The catalytic reforming step that can be used to obtain the reformate renewable component according to the invention can be conducted according to processes known in the art, for example at a temperature ranging from 480°C to 510°C, taking into account that the Applicant has also found that as the catalytic reforming temperature to which the heavy renewable naphtha of the present invention is subjected increases, the concentration of aromatics produced increases . The catalyst used in the catalytic reforming step can be any catalytic reforming catalyst known in the art, such as, for example, a catalyst based on molybdenum and aluminium in oxide form, a platinum catalyst on acid carrier, a bimetallic catalyst based on platinum and rhenium, a bi-funct ional catalyst containing platinum, rhodium with alumina.

[0166] As mentioned above, the reformate renewable component and the isomerated renewable component described above according to the invention can be blended together in order to obtain a renewable base gasoline from which to obtain a gasoline fuel formulation comprising not only the base gasoline but also one or more other components and / or additives (e.g. oxygenated components, antioxidants, detergents, and the like) used to achieve the technical characteristics required of a gasoline fuel formulation to be marketed as a fuel in accordance with EN228 or to achieve other technical specifications required by specific fields of use such as, for example, a higher oxygen content than that indicated in EN228.

[0167] Another object of the present invention is therefore a base gasoline comprising or consisting of

[0168] - at least one reformate renewable base component as defined above with a RON of at least 95, preferably a

[0169] RON of at least 100; - at least one renewable isomerate base component as defined above; wherein the volume ratio between the aforesaid reformate component and the aforesaid isomerate component is greater than, or at least equal to, 1.5, preferably ranging from 1.70 to 3, more preferably from 1.75 to 2, even more preferably equal to 1.85.

[0170] It is to be understood that it is possible to use volume ratio lower than 1.5 between the aforesaid reformate component and the aforesaid isomerate component, without departing from the scope of the present invention.

[0171] This renewable base gasoline exhibits a RON of at least 95, preferably a RON of at least 100.

[0172] Moreover, this renewable base gasoline has a density ranging from 735 to 765 kg / m3.

[0173] This renewable base gasoline exhibits a vapour pressure ranging from 50 kPa to 75 kPa, said vapour pressure being preferably measured according to EN 13016.

[0174] This renewable base gasoline exhibits:

[0175] - a distillation temperature T5%vol which can range from 40°C to 48°C;

[0176] - a distillation temperature T50%vol which can range from 78°C to 90°C; - a distillation temperature T90%vol which can range from 150°C to 160°C;

[0177] - F.B.P. which can range from 197°C to 207°C.

[0178] The aforesaid renewable base gasoline also exhibits:

[0179] - an evaporation value at 70°C which can range from 20% to 50% by volume with respect to the total volume of the mixture (%v / v) , preferably 35% to 45% by volume;

[0180] - an evaporation value at 100°C which can range from 46% to 72% by volume with respect to the total volume of the mixture (%v / v) , preferably from 55% to 60% by volume .

[0181] These evaporation values are in accordance with EN 228.

[0182] In an embodiment, the renewable base gasoline having a RON of at least 95 according to the invention comprises or is preferably composed of:

[0183] - 64% v / v of renewable reformate component as defined above having an octane number (RON) value of at least 95, preferably greater than or equal to 100;

[0184] - 36% v / v of renewable isomerate component as defined above .

[0185] In a preferred embodiment, the aforesaid renewable base gasoline having a RON of at least 95 is composed of the two aforesaid components in a ratio of 64 / 36 vol / vol in which the reformate component as defined above has a RON of at least 100. In another preferred embodiment, the renewable base gasoline has a RON of at least 95, consists of 64% vol / vol of a reformate renewable base component having the characteristics shown in Table 1 and 36% vol / vol of a renewable isomerate base component having the characteristics shown in Table 5.

[0186] In this preferred embodiment, the renewable base gasoline has the characteristics shown in Table 6. Table 6: Renewable base gasoline characteristics

[0187] In an embodiment, the renewable base gasoline according to the invention is blended with:

[0188] - at least one oxygenated component of fossil nature or of a renewable nature, preferably of a renewable nature, which includes an alcohol with a number of carbon atoms ranging from 1 to 4, preferably 2 to 3, more preferably ethanol, even more preferably ethanol of a renewable nature , to obtain a gasoline fuel formulation comprising a reformate renewable base component and a renewable isomerate base component as defined above and one or more oxygenated compounds as defined above.

[0189] An example of ethanol of a renewable nature is the "cellulosic ethanol" produced from biomass residues, e.g. from lignocellulose, by means of known processes. In an embodiment, this gasoline fuel formulation comprises said renewable base gasoline and said oxygenated compound, where said oxygenated compound is present in quantities of less than 20% by volume with respect to the total volume of the formulation.

[0190] The gasoline fuel formulation in accordance with the invention comprising a reformate renewable base component in accordance with the invention, an isomerate renewable base component in accordance with the invention and optionally an oxygenated component as defined above may also contain additional additives or gasoline components other than the oxygenated component to comply with the EN228 specification for gasoline distributed at the pump.

[0191] Another object of the present invention is therefore a gasoline fuel formulation or composition comprising

[0192] - at least one reformate renewable base component as defined above with a RON of at least 95, preferably a RON of at least 100; at least one renewable isomerate base component as defined above; and

[0193] - at least one oxygenated component of fossil nature or of a renewable nature, preferably of a renewable nature, which includes an alcohol with a number of carbon atoms ranging from 1 to 4, preferably 2 to 3, more preferably ethanol, even more preferably ethanol of a renewable nature , wherein the volume ratio between the reformate component and the isomerate component is greater than, or at least equal to, 1.5, preferably 1.70 to 3, more preferably 1.75 to 2, even more preferably 1.85.

[0194] In a preferred embodiment, this gasoline fuel formulation has a RON of at least 95, preferably ranging from 95 to 102, more preferably ranging from 100 to 102, and comprises or consists of:

[0195] - 52% v / v of reformate base component of a fully renewable nature as defined above, preferably reformate renewable component having a RON of at least 100 as defined above;

[0196] - 29.2% v / v of isomerate base component of fully renewable nature as defined above;

[0197] - 18.8 % v / v of an oxygenated component of a fully renewable nature, preferably an alcohol with 1 to 4 carbon atoms, preferably 2 to 3, more preferably ethanol, the sum of the three components being equal to 100% vol.

[0198] In a preferred embodiment, the aforementioned fuel formulation of gasoline 52-29.20-18.80 v / v / v comprises ethanol, preferably ethanol of renewable origin, as an oxygenated component . This preferred fuel formulation of fully renewable gasoline (52-29.20-18.80 v / v / v) with a RON ranging from 100 to 102 exhibits:

[0199] - a vapour pressure which can range from 45 to 68 kPa (EN 13016) ;

[0200] - a boiling point T10 %vol which can range from 45°C to 50°C;

[0201] - a boiling point T90% vol which can range from 148°C to 153°C;

[0202] - an I.B.P. which can range from 36°C to 42°C;

[0203] - an F.B.P which can range from 197°C to 210°C.

[0204] In an embodiment, the fuel formulation 52-29.20-18.80 v / v / v consists of the reformate renewable base component and the isomerate renewable base component, which have the properties as shown in Table 1 and Table 5, respectively, and shows the following properties as shown in Table 7.

[0205] Table 7 : Characteristics of a high-octane renewable gasoline fuel formulation (52 / 29.20 / 18.80 v / v / v)

[0206] The above-mentioned preferred formulation with the characteristics listed in Table 7 meets the demand for gasolines that are of fully renewable origin and can be used in competition gasoline engines, which must have

[0207] - an octane number (RON) value of at least 95, preferably greater than or equal to 100;

[0208] - an oxygen content of at least 6.7% by weight with respect to the total weight of the mixture (%m / m) , up to a maximum of 7.1% by weight.

[0209] One of the advantages of the renewable gasoline fuel formulation according to the present invention is that it can enable CO2emissions, based on a Life Cycle Assessment (LCA) , which are reduced compared to traditional fossil- based gasoline. It is estimated that this bio-gasoline, according to an LCA evaluation, allows for a significant reduction in C02emissions, e.g. , from 60% to 80%, compared to traditional fossil-based gasoline.

[0210] As is clear from what has been described so far, starting from a single naphtha cut of renewable origin, it is possible to obtain, after a conventional splitting step, two different naphtha cuts that successively give rise to

[0211] - a renewable isomerate base component derived from an isomerization step, e.g. as described above, and

[0212] - a reformate renewable base component derived from a catalytic reforming step, e.g. from catalytic reforming as described above, resulting in a high RON base gasoline .

[0213] Another object of the present invention is therefore an integrated process for producing a gasoline fuel formulation comprising a reformate renewable base component of gasoline and an isomerate renewable base component of gasoline, said process comprising the steps of:

[0214] (A) Subjecting a starting renewable naphtha (HVO Naphtha) with a high isoparaffin content to a fractionation process (splitting) , said starting naphtha comprising hydrocarbons having from 4 to 12 carbon atoms, and having an I.B.P. ranging from 25°C to 45°C and an F.B.P. ranging from 165°C to 175°C;

[0215] - an iso-paraffinic hydrocarbon content of at least 35% by weight of the total weight of hydrocarbons;

[0216] - a naphthene content lower than 20% by weight of the weight of total hydrocarbons;

[0217] - an aromatic content lower than 5% by weight of the weight of total hydrocarbons; obtaining the separation of a first mixture of hydrocarbons mainly comprising hydrocarbons having a number of carbon atoms greater than 6 (heavy renewable naphtha) from a second mixture of hydrocarbons (light renewable naphtha) mainly comprising hydrocarbons having a number of carbon atoms lower than 7;

[0218] (B) Subjecting said renewable heavy naphtha to catalytic reforming to obtain a renewable reformate base component with a RON of at least 95 as defined above;

[0219] (C) Subjecting said light renewable naphtha to isomerization to obtain a renewable isomerate base gasoline component as defined above;

[0220] (D) Mixing said isomerate renewable base gasoline component obtained in step (C) and said reformate renewable base gasoline component obtained in step (B) to obtain a base gasoline, preferably a base gasoline having a volumetric ratio of reformate component / isomerate component greater than or at least equal to 1.5;

[0221] (E) Optionally adding to said base gasoline at least one oxygenated component of fossil nature or of renewable nature, preferably of renewable origin, comprising an alcohol having a number of carbon atoms ranging from 1 to 4, preferably 2 to 3, more preferably ethanol, even more preferably ethanol of renewable nature, to obtain a gasoline fuel composition as described above comprising said base gasoline and said oxygenated component ; and / or

[0222] (F) optionally adding one or more other gasoline components or additives to the fuel composition obtained in (E) ; to obtain a gasoline fuel formulation, preferably a gasoline fuel formulation as defined above.

[0223] In step (A) , said first mixture is preferably the heavy renewable naphtha defined above and said second mixture is preferably the light renewable naphtha defined above.

[0224] In an embodiment, in step (A) of the integrated process described above, said first mixture is a heavy renewable naphtha with a high iso-paraffin content in the form of a hydrocarbon mixture not containing benzene and comprising paraffinic, naphthenic and aromatic hydrocarbons, said heavy renewable naphtha having the following characteristics

[0225] - an I.B.P. ranging from 95°C to 105°C, preferably from 99°C to 102°C;

[0226] - an F.B.P. ranging from 190°C to 200°C, preferably 193°C to 196°C;

[0227] - an isoparaffin content of at least 35% by weight with respect to the weight of the total hydrocarbons;

[0228] - a naphthene content lower than 30% by weight of the weight of total hydrocarbons;

[0229] - an aromatic content lower than 5% by weight of the weight of total hydrocarbons; and said second mixture is a light renewable naphtha comprising hydrocarbons having a carbon atom number ranging from 3 to 7 and having

[0230] - an I.B.P. ranging from 33°C to 36°C;

[0231] - an F.B.P. ranging from 70°C to 73°C;

[0232] - a boiling point T10 %vol / vol ranging from 41°C to 45°C;

[0233] - a boiling point T95 % vol / vol ranging from 65°C to 68°C;

[0234] - an iso-paraffin content greater than 40% by weight with respect to the total weight of the hydrocarbons, preferably ranging from 60% to 70% by weight.

[0235] The aforesaid fractionation (splitting) , catalytic reforming and isomerization steps can be conducted under the same conditions as described above, but this is not binding for the purposes of the present invention.

[0236] In particular,

[0237] - the splitting step can be conducted at atmospheric pressure ;

[0238] - the reforming step can be conducted at a temperature ranging from 480°C to 510°C, operating at moderate pressures, e.g. ranging from 4 bar to 30 bar, and in the presence of H2, using any reforming catalyst used for reforming fossil fuels such as those described above ;

[0239] - the process of isomerization of linear alkane hydrocarbons is known in the art and is generally conducted at a temperature of 240-250°C and a pressure of approximately 15-20 barg, in the presence of conventional isomerization catalysts such as those described above.

[0240] Said integrated process may also include one or more steps of obtaining the starting renewable naphtha to be subjected to step (A) as defined above, starting from biological feedstocks from renewable sources such as, for example, the deoxygenation, isomerization and distillation steps provided for in the known processes of hydrotreatment of vegetable oils or other renewable feedstocks, such as, for example the hydrotreatment process defined as Ecofining™ described above.

[0241] In particular, in an embodiment of said integrated process in accordance with the invention, it may be contemplated, prior to step (A) , to carry out a step (AO) of obtaining said starting renewable naphtha by catalytic hydrotreatment of a biological feedstock of renewable origin selected from vegetable oils, exhausted cooking oils, animal fats and the like, said hydrotreatment comprising a catalytic hydrodeoxygenation step in the presence of H2 and an isomerization step of the deoxygenated product.

[0242] By way of example, the integrated process steps for obtaining gasoline fuel according to the invention are shown in Figure 1.

[0243] In another embodiment of the aforesaid integrated process according to the invention, an optional desulfurization step (Al) of the starting renewable naphtha (if necessary, depending on the sulphur content) which has previously been obtained from a process for converting biological feedstocks from renewable sources into hydrocarbons as described above as step (AO) may be carried out prior to the splitting step (A) .

[0244] This desulfurization process can be analogous to those in the art for the treatment of fossil fuels. DESCRIPTION OF THE DRAWINGS

[0245] Figure 1 represents a diagram illustrating, in block form, the aforesaid steps (AO) , (A) , (B) , (C) , (D) , (E) of the above-described integrated process in accordance with the invention, including the steps for converting a vegetable oil into naphtha by means of the above-described hydrotreatment process (AO) .

[0246] The fully renewable origin of the reformate and isomerate base components of the gasoline fuel formulation according to the invention can be determined by quantifying radiocarbon 14 which is absent in materials of fossil origin. This analysis can be conducted by means of SCAR spectroscopy, accelerated mass spectrometry (AMS) or the like.

[0247] Examples of suitable methods for analysing the carbon content of renewable / organic origin that can be used are DIN 51637 (2014) , EN 16640 (2017) , ASTM D6866 (2018) .

[0248] Generally, a product is considered to be of renewable origin if it contains more than 90% carbon of renewable origin or carbon referred to as "modern carbon" (pMC) .

Claims

CLAIMS1. Renewable base component having a high RON and high isoparaffin content of a gasoline fuel characterized by being a reformed ("Reformate") renewable component having a RON of at least 95, preferably from 95 to 105, said reformate renewable component being a mixture of hydrocarbons comprising aromatic hydrocarbons, naphthenes (i.e. saturated cyclic hydrocarbons) , linear paraffins, isoparaffins, wherein the iso-paraffins content varies from 10% by weight to 35% by weight with respect to the weight of the total hydrocarbons, preferably from 15% by weight to 25% by weight, more preferably greater than 18% by weight, said reformate renewable base component having- an I.B.P. ranging from 30°C to 50°C;- an F.B.P. ranging from 190°C to 220°C;- a boiling point T10 %vol ranging from 60°C to 90°C;- a boiling point T20 %vol ranging from 80°C to 105°C;- a boiling point T90 %vol ranging from 150°C to 170°C.

2. Reformate renewable component according to claim 1 further having- a boiling point T30 %vol ranging from 97°C to 117°C;- a boiling point T70 %vol ranging from 128°C to 142°C;- a boiling point T80 %vol ranging from 140°C to 150°C.

3. Reformate renewable component according to claim 1 or 2, wherein the olefin content is less than 3% by weight based on the weight of the total hydrocarbons.

4. Reformate renewable component according to any one of the preceding claims, wherein the concentration of benzene is less than 2% by weight with respect to the weight of the total hydrocarbons, preferably less than 1, 5%, said concentration being able to be also zero.

5. Reformate renewable component according to any one of the preceding claims 1 to 4, characterized in that it is derived from a renewable naphtha (HVO-HVN) with a high isoparaffin content which is a mixture of hydrocarbons not containing benzene and comprising paraffinic, naphthenic, aromatic hydrocarbons, said renewable naphtha (HVO-HVN) having the following characteristics- an I.B.P. ranging from 95°C to 105°C, preferably from 99°C to 102°C;- an F.B.P. ranging from 190°C to 200°C, preferably from 193°C to 196°C;- an isoparaffin content equal to at least 35% by weight with respect to the weight of the total hydrocarbons;- a naphthene content less than 30% by weight with respect to the weight of the total hydrocarbons;- an aromatics content of less than 5% by weight with respect to the weight of total hydrocarbons.

6. Renewable base gasoline consisting of- a reformate renewable base component having a RON of at least 95, preferably a RON of at least 100, as defined in any one of the preceding claims;- an isomerate base component of renewable origin in the form of a mixture of hydrocarbons comprising iso-paraffins, aromatic hydrocarbons, naphthenes, n-paraffins and having- an I.B.P. ranging from 32°C to 35°C;- an F.B.P. ranging from 73°C to 78°C;- a boiling point T10 %vol ranging from 38°C to 42°C, preferably from 39°C to 42°C;- a boiling point T60 %vol ranging from 43°C to 49°C;- a boiling point T70 %vol ranging from 47°C to 53°C;- a boiling point T95% vol ranging from 57°C to 65°C;- a naphthene content of less than 5% by weight with respect to the weight of the total hydrocarbons, said reformate renewable base component and said renewable isomerate base component being in a volumetric ratio greater than or at least equal to 1.5, preferably from 1.75 to 2.5, more preferably 1.85.

7. Fully renewable gasoline fuel composition comprising- a base gasoline as defined in preceding claim 6wherein said reformate component and said isomerate component of said base gasoline are in a volumetric ratio greater than or at least equal to 1.5, preferably from 1.75 to 2.5, more preferably 1.85.

8. Fuel composition according to claim 7, wherein said fuel composition further comprises- at least one oxygenated component of fossil or renewable nature, preferably of renewable nature, which includes an alcohol having a number of carbon atoms ranging from 1 to 4, preferably from 2 to 3, more preferably ethanol, even more preferably ethanol of renewable origin.

9. Fuel composition according to claim 8, wherein said oxygenated component is present in quantities lower than 20% by volume with respect to the total volume of the composition, said oxygenated component being preferably of renewable origin.

10. Fuel composition according to any one of the preceding claims 7 to 9, wherein additional gasoline additive components other than oxygenated compounds are present.

11. Gasoline fuel composition according to any one of the preceding claims 7 to 10, comprising or consisting of- 52% v / v of a reformate renewable base gasoline component having a RON of at least 100, as defined in any of the preceding claims;29.2% v / v of a renewable isomerate base component asdefined in any of the preceding claims;- 18.8% v / v of an oxygenated component of a completely renewable nature, preferably an alcohol with a carbon number of atoms between 1 and 4, more preferably an alcohol with a carbon number of atoms between 2 and 3, even more preferably ethanol , said gasoline fuel composition having a RON of at least 95, preferably from 95 to 102, more preferably ranging from 100 to 102.

12. Process for preparing a reformate renewable base component as defined in any one of the preceding claims 1 to 5 of the gasoline fuel as defined in claim 6, said process comprising subjecting to catalytic reforming a naphtha of renewable origin (HVO-HVN) having a high isoparaffin content which does not contain benzene and comprises paraffinic, naphthenic, aromatic hydrocarbons, said renewable naphtha (HVO-HVN) having the following characteristics- an I.B.P. ranging from 95°C to 105°C, preferably from 99°C to 102°C;- an F.B.P. ranging from 190°C to 200°C, preferably from 193°C to 196°C;- an isoparaffin content of at least 35% by weight with respect to the weight of the total hydrocarbons;- a naphthene content of less than 30% by weight of the total hydrocarbons;- an aromatic content of less than 5% by weight of the total hydrocarbons.

13. Process for preparing an isomerate renewable base component as defined in claim 5 of the gasoline fuel as defined in claim 6, said process comprising subjecting to isomerization a naphtha of renewable origin (HVO-LVN) comprising hydrocarbons having a number of carbon atoms ranging from 3 to 7 and having- an I.B.P. ranging from 33°C to 36°C;- an F.B.P. ranging from 70°C to 73°C;- a boiling temperature T10 %vol / vol ranging from 41°C to 45°C;- a boiling temperature T95 % vol / vol ranging from 65°C to 68 °C;- an iso-paraffin content greater than 40% by weight with respect to the total weight of the hydrocarbons, preferably ranging from 60% to 70% by weight.

14. Integrated process for the production of a gasoline fuel composition as defined in claim 6 comprising- a reformate renewable base component of gasoline as defined in the preceding claims 1-5; and- an isomerate renewable base component of gasoline as defined in the preceding claim 6,said process comprising the steps of(A) subjecting to splitting a starting renewable naphtha (HVO Naphtha) with a high isoparaffin content and having- an I.B.P. ranging from 25°C to 45°C, and F.B.P. ranging from 165°C to 176°C;- an isoparaffin content of at least 35% by weight with respect to the weight of the total hydrocarbons ;- a naphthene content of less than 20% by weight with respect to the weight of the total hydrocarbons;- an aromatics content of less than 5% by weight with respect to the weight of the total hydrocarbons; preferably said starting renewable naphtha (HVO Naphtha) having a RON of at least 35, to obtain a first mixture of hydrocarbons predominantly comprising hydrocarbons having a carbon number greater than 6 (heavy renewable naphtha) and a second mixture of hydrocarbons (light renewable naphtha) predominantly comprising hydrocarbons having a carbon number less than 7 ; said first mixture being preferably a high isoparaffin content renewable naphtha (HVO-HVN) as defined in claim 4 and / or 11, and said second mixture being preferably a high isoparaffin content renewable naphtha (HVO-LVN)as defined in claim 12;(B) subjecting said heavy renewable naphtha to catalytic reforming to obtain a reformate gasoline component having a RON of at least 95 and having the characteristics as defined in any one of the preceding claims 1-4;(C) subjecting said light renewable naphtha to isomerization to obtain an isomerate gasoline component having the characteristics as defined in claim 5;(D) Mixing said isomerate gasoline component obtained in step (C) and said reformate renewable gasoline component obtained in step (B) to obtain a base gasoline, preferably a renewable base gasoline having a reformate component / isomerate component volume ratio greater than or at least equal to 1.5;(E) optionally adding to said base gasoline at least one oxygenated component of fossil or renewable nature, preferably renewable nature, which includes an alcohol having a carbon number ranging from 1 to 4, to obtain a gasoline fuel composition as defined in any of the preceding claims comprising said base gasoline and said oxygenated component; and / or(F) optionally adding to the fuel composition obtained in(E) one or more other gasoline components or additives.

15. Process according to claim 14, wherein prior to step (A) a step (AO) is provided for obtaining said starting renewable naphtha by catalytic hydrotreatment of a renewable feedstock selected from vegetable oils, exhausted cooking oils, animal fats and the like, said hydrotreatment comprising a catalytic deoxygenation step in the presence of H2 and an isomerization step of the deoxygenated product.

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