NAPHTHENIC BIOSOURCES FLUIDS

Abstract

The invention relates to a process for preparing a naphthenic fluid, said process comprising a step of hydrogenating a hydrocarbon feedstock comprising: - 5 to 40% by mass of naphthenes, - 50 to 90% by mass of non-cyclic paraffins, and - 1 to 10% by mass of aromatic compounds, relative to the total mass of the hydrocarbon feedstock, said hydrocarbon feedstock having a biocarbon content greater than or equal to 90% by mass, relative to the total mass of carbon in the hydrocarbon feedstock. The invention also relates to a naphthenic fluid as such.

Description

Title of the invention: NAPHTHENIC BIOSOURCE FLUIDS TECHNICAL FIELD OF THE INVENTION

[0001] The invention relates to a process for preparing a naphthenic fluid from a hydrocarbon feed of biological origin and a naphthenic fluid obtained from a biological feed. STATE OF THE ART

[0002] Special fluids are liquids used as industrial fluids, agricultural fluids, and domestic fluids generally obtained from fossil hydrocarbons transformed by refining processes but also from many products from roligomerization of 2- to 4-carbon olefins and also from synthetic hydrocarbons resulting from the transformation of natural gas or synthesis gas from biomass and / or coal.Among these, we find drilling fluids, industrial lubricants, fluids for automotive formulations, plant protection products, base fluids for ink formulations, fuels for domestic applications, extending oils for sealants, viscosity reducers for resin-based formulations, pharmaceutical compositions and compositions for food contact, fluids for cosmetic formulations, heat transfer fluids, dielectric fluids, lubricant base fluids, degreasing fluids.

[0003] Manufacturers are increasingly seeking to replace products of fossil origin with bio-based products (which are not of fossil origin).

[0004] Document WO2016185047 describes a heavy HDO / ISO component having more than 95% by mass of isoparaffins and less than 100 ppm of aromatics, obtained by a hydrodeoxygenation and hydroisomerization process of biomass. The fluids described in this document are highly isoparaffinic fluids.

[0005] The present invention aims to provide a process for preparing a bio-based naphthenic fluid and a bio-based naphthenic fluid having a composition and properties suitable for the intended applications. Summary of the invention

[0006] The invention relates to a process for preparing a naphthenic fluid, said process comprising a step of hydrogenating a hydrocarbon feedstock comprising:

[0007] - 5 to 40% by mass of naphthenes,

[0008] - from 50 to 90% by mass of non-cyclic paraffins, and

[0009] - from 1 to 10% by mass of aromatic compounds,

[0010] in relation to the total mass of the hydrocarbon charge,

[0011] said hydrocarbon charge having a biocarbon content greater than or equal to 90% by mass, relative to the total mass of carbon in the hydrocarbon charge.

[0012] According to one embodiment of the process according to the invention, the hydrocarbon feed comprises at least 70% by mass, preferably 100% by mass, of one or more components of biological origin, relative to the total mass of the hydrocarbon feed, at least one component of biological origin preferably being from a kraft process.

[0013] Preferably, the biologically derived component obtained from a kraft process comprises:

[0014] - 20 to 40% by mass of naphthenes,

[0015] - 50 to 75% by mass of non-cyclic paraffins, and

[0016] - from 4 to 10% by mass of aromatic compounds,

[0017] compared to the total mass of the biologically derived component obtained from a kraft process,

[0018] preferably the isoparaffins / n-paraffins mass ratio of the biologically derived component from a kraft process ranges from 1 to 8, preferably from 1.5 to 4.

[0019] According to one embodiment of the process according to the invention, the hydrocarbon feedstock has one or more of the following characteristics:

[0020] - a naphthenes content ranging from 10 to 35% by mass relative to the total mass of the hydrocarbon charge, and / or

[0021] - a non-cyclic paraffin content ranging from 60 to 90% by mass relative to the total mass of the hydrocarbon load, and / or

[0022] - an aromatic compound content ranging from 2 to 10% by mass relative to the total mass of the hydrocarbon load, and / or

[0023] - a biocarbon content greater than or equal to 95% by mass relative to the total carbon mass of the hydrocarbon feedstock, and / or

[0024] - an initial boiling point in the range of 50 to 250°C, preferably of 100 to 200°C, and / or

[0025] - a final boiling point in the range of 150 to 400°C, preferably of 200 to 390°C, and / or

[0026] - a boiling range having a width greater than or equal to 50°C, preferably greater than or equal to 100°C, and / or

[0027] - a kinematic viscosity at 40°C less than or equal to 10 cSt, preferably less than or equal to 5 cSt.

[0028] According to one embodiment of the process according to the invention, the naphthenic fluid has an aromatics content of less than or equal to 500 ppm by mass, preferably less than or equal to 300 ppm by mass, preferably even less than or equal to 100 ppm by mass, relative to the total mass of the naphthenic fluid.

[0029] According to one embodiment, the process according to the invention further comprises a distillation step carried out before the hydrogenation step and / or after the hydrogenation step.

[0030] According to one embodiment of the process according to the invention, the hydrocarbon filler comprises a mass ratio of isoparaffins / n-paraffins ranging from 1 to 11, preferably from 1.5 to 10.

[0031] According to a first embodiment of the process according to the invention, the hydrocarbon feed comprises, or even consists of:

[0032] - from 30 to 90% by mass, preferably from 40 to 70% by mass, of a component of biological origin, produced using a kraft paper process, and

[0033] - from 10 to 70% by mass, preferably from 30 to 60% by mass, of a component of biological origin, obtained through a hydrodeoxygenation and hydroisomerization process of a vegetable or animal oil,

[0034] in relation to the total mass of the hydrocarbon charge.

[0035] Preferably, the biologically derived component obtained from a hydrodeoxygenation and hydroisomerization process of a vegetable or animal oil comprises:

[0036] - at least 75% by mass of isoparaffins,

[0037] - less than 25% by mass of n-paraffins,

[0038] - less than 1% by mass of aromatics, and

[0039] - less than 1% by mass of naphthenes,

[0040] compared to the total mass of the biologically derived component obtained from a hydrodeoxygenation and hydroisomerization process of a vegetable or animal oil,

[0041] preferably the isoparaffins / n-paraffins mass ratio of the biologically derived component from a hydrodeoxygenation and hydroisomerization process of a vegetable or animal oil ranges from 1.5 to 11, preferably from 2 to 10.

[0042] According to a second embodiment of the process according to the invention, the hydrocarbon filler comprises 100% by mass of a component of biological origin obtained from a kraft process.

[0043] The invention also relates to a naphthenic fluid comprising:

[0044] a) a biocarbon content greater than or equal to 90% by mass relative to the total mass of carbon atoms in the naphthenic fluid,

[0045] b) a naphthene content ranging from 6 to 50% by mass, relative to the total mass of the naphthenic fluid,

[0046] c) a non-cyclic paraffin content ranging from 50 to 90% by mass, relative to the total mass of the naphthenic fluid,

[0047] d) an aromatics content less than or equal to 500 ppm by mass, relative to the total mass of the naphthenic fluid.

[0048] According to an embodiment of the naphthenic fluid according to the invention, the aromatics content is less than or equal to 500 ppm by mass, preferably less than or equal to 300 ppm by mass, preferably even less than or equal to 100 ppm by mass, relative to the total mass of the naphthenic fluid.

[0049] According to a first embodiment, the naphthenic fluid according to the invention comprises:

[0050] a) a biocarbon content greater than or equal to 95% by mass relative to the total mass of carbon atoms in the naphthenic fluid,

[0051] b) a naphthene content ranging from 20 to 50% by mass, relative to the total mass of the naphthenic fluid,

[0052] c) a non-cyclic paraffin content ranging from 50 to 75% by mass, relative to the total mass of the naphthenic fluid,

[0053] d) an aromatics content less than or equal to 100 ppm by mass, relative to the total mass of the naphthenic fluid,

[0054] preferably the isoparaffins / n-paraffins mass ratio of the naphthenic fluid ranges from 1 to 8, preferably from 1.5 to 4.

[0055] According to a first embodiment, the naphthenic fluid according to the invention comprises:

[0056] a) a biocarbon content greater than or equal to 95% by mass relative to the total mass of carbon atoms in the naphthenic fluid,

[0057] b) a naphthene content ranging from 6 to 40% by mass, relative to the total mass of the naphthenic fluid,

[0058] c) a non-cyclic paraffin content ranging from 60 to 90% by mass, relative to the total mass of the naphthenic fluid,

[0059] d) an aromatics content less than or equal to 100 ppm by mass, relative to the total mass of the naphthenic fluid,

[0060] preferably the isoparaffins / n-paraffins mass ratio of the naphthenic fluid ranges from 1.5 to 11, preferably from 2 to 10.

[0061] The invention also relates to the use of a naphthenic fluid obtained by the process according to the invention or of a naphthenic fluid according to the invention, as a drilling fluid, as a solvent, in particular for ink, paint, resin, adhesive, as an oil for sealants, as a thermal fluid or as an additive in fuel formulation, preferably as an oil for sealants and / or as a solvent for ink, paint, resin and / or adhesive.

[0062] The invention makes it possible to provide a naphthenic fluid from a bio-based feedstock having particularly advantageous properties. DETAILED DESCRIPTION OF THE INVENTION

[0063] The invention relates to a process for preparing a naphthenic fluid, said process comprising a step of hydrogenating a hydrocarbon feedstock comprising:

[0064] - from 5 to 40% by mass of naphthenes,

[0065] - from 50 to 90% by mass of non-cyclic paraffins, and

[0066] - from 1 to 10% by mass of aromatic compounds,

[0067] in relation to the total mass of the hydrocarbon feed,

[0068] said hydrocarbon feedstock having a biocarbon content greater than or equal to 90% by mass relative to the total mass of carbon in the hydrocarbon feedstock.

[0069] Advantageously, the process includes a distillation step carried out before the hydrogenation step and / or after the hydrogenation step, preferably after the hydrogenation step.

[0070] The distillation step typically allows one or more cuts to be prepared having a distillation range of less than 100°C, advantageously ranging from 10 to 80°C.

[0071] Thus, the naphthenic fluid can correspond to the top cut, an intermediate cut or the bottom cut after distillation.

[0072] As a preliminary point, it should be noted that, in the following description and claims, the expression "between" should be understood as including the limits mentioned.

[0073] For the purposes of the present invention, the word "paraffins" means branched alkanes (also called iso-paraffins or iso-alkanes) and unbranched alkanes (also called n-paraffins or n-alkanes).

[0074] For the purposes of the present invention, the word "isoparaffins" refers to non-cyclic branched alkanes.

[0075] For the purposes of the present invention, the word "n-paraffins" refers to non-cyclic linear alkanes.

[0076] For the purposes of the present invention, the word "naphthenes" refers to cyclic alkanes or cycloalkanes (non-aromatic), typically containing 5 to 11 carbon atoms.

[0077] In the context of the present invention, the boiling point is determined according to ASTM D86. Hydrocarbon charge

[0078] The process of the invention uses a hydrocarbon filler.

[0079] The hydrocarbon feedstock has a biocarbon content greater than or equal to 90% by mass, preferably greater than or equal to 95% by mass, and preferably even greater than 100% by mass, relative to the total mass of carbon in the hydrocarbon feedstock. This characteristic typically results from the choice of the feedstock's origin, in particular its biological origin. Thus, said hydrocarbon feedstock is typically of biological origin.

[0080] The biocarbon content (also referred to as bio-sourced carbon or biogenic carbon) can be determined according to ASTM D6866 of 2020.

[0081] The hydrocarbon filler used in the invention has a naphthenes content ranging from 5 to 40% by mass, preferably from 10 to 35% by mass, relative to the total mass of the hydrocarbon filler.

[0082] The hydrocarbon filler used in the invention has a non-cyclic paraffin content ranging from 50 to 90% by mass, preferably from 60 to 90% by mass, relative to the total mass of the hydrocarbon filler.

[0083] The hydrocarbon filler used in the invention has an aromatic compound content ranging from 1 to 10% by mass, preferably from 2 to 10% by mass, relative to the total mass of the hydrocarbon filler.

[0084] The naphthenes, paraffins including n-paraffins and isoparaffins, and aromatic compounds content of the feed can be determined by gas chromatography according to any method known to those skilled in the art.

[0085] According to one embodiment, the ratio between the mass proportion of isoparaffins and the mass proportion of n-paraffins in the hydrocarbon filler ranges from 1 to 11, preferably from 1.5 to 10.

[0086] Advantageously, the hydrocarbon charge has an extremely low mass content of sulfur compounds, typically less than or equal to 15 ppm, preferably less than or equal to 10 ppm and more preferably less than or equal to 5 ppm.

[0087] Advantageously, the hydrocarbon filler also has a kinematic viscosity at 40°C less than or equal to 10 cSt, preferably less than or equal to 5 cSt, measured for example according to ASTM D445.

[0088] Preferably, the hydrocarbon charge has an initial boiling point and a final boiling point in the range of 130 to 400°C, preferably from 150 to 375°C.

[0089] A not too high final boiling point for the hydrocarbon charge makes it possible to increase the life of the catalyst and to have a lasting decrease in the aromatic content.

[0090] According to a particular embodiment, the hydrocarbon charge has an initial boiling point ranging from 150 to 250°C and a final boiling point ranging from 260 to 380°C.

[0091] According to this embodiment, a distillation will advantageously be carried out after hydrogenation in order to obtain a naphthenic fluid having a narrow distillation range.

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[0102] The hydrocarbon load advantageously comprises at least 70% by mass, preferably 100% by mass, of one or more components of biological origin, relative to the total mass of the hydrocarbon load. According to a particularly preferred embodiment, the hydrocarbon filler used in the invention comprises at least one component of biological origin obtained through a kraft process. Preferably, the hydrocarbon filler used in the invention comprises at least 30% by mass, and preferably at least 40% by mass, of a component of biological origin obtained through a kraft process, relative to the total mass of the hydrocarbon filler. The biological component from a Kraft process can be obtained, for example, by pretreating tall oil to remove water and salts, followed by hydrotreatment (with hydrogen) to remove water, hydrogen sulfide, and other heteroatoms. This tall oil can be a viscous liquid obtained as a by-product of the Kraft process for manufacturing wood pulp, during the pulping of primarily coniferous trees. The Kraft process includes a cooking step. The hydrotreated effluent can be distilled to separate the gas and possibly the naphtha. A method for preparing a hydrocarbon feedstock that can be implemented in the present invention is described for example in document WO2011 / 148046. According to a particular embodiment, the biologically derived component produced by a kraft process comprises: - 20 to 40% by mass of naphthenes, - 50 to 75% by mass of non-cyclic paraffins, and - 4 to 10% by mass of aromatic compounds, compared to the total mass of the biologically sourced component obtained through a kraft process. Preferably, the ratio between the mass proportion of isoparaffins and the mass proportion of n-paraffins in the biological component from a kraft process is from 1 to 8, preferably from 1.5 to 4. For example, the bio-based component produced using a kraft process may include: - 35 to 50% by mass of isoparaffins, and - 10 to 30% by mass of n-paraffins, compared to the total mass of the biologically sourced component obtained through a kraft process. According to one embodiment, the bio-based component produced by a kraft process has a bio-carbon content of at least 60% by mass, preferably at least 80% by mass, preferably even at least 90% by mass, relative to the total mass of carbon atoms of the biologically sourced component produced by a kraft process.

[0103] The biological component obtained from a kraft process also preferably has an extremely low mass content of sulfur compounds, typically less than or equal to 15 ppm, preferably less than or equal to 10 ppm and more preferably less than or equal to 5 ppm.

[0104] The biological component obtained from a kraft process also preferably has a kinematic viscosity at 40°C less than or equal to 10 cSt, preferably less than or equal to 5 cSt, measured for example according to ASTM D445.

[0105] Preferably, the biologically derived component from a kraft process has an initial boiling point and a final boiling point in the range of 130 to 400°C, preferably from 150 to 380°C.

[0106] Boiling points can be determined according to ASTM D86.

[0107] The biologically derived component obtained from a kraft process also preferably has an aniline point less than or equal to 90°C, preferably ranging from 50 to 80°C, measured for example according to ASTM D611. The biologically derived component obtained from a kraft process has a particularly low aniline point, especially in comparison with a hydrocarbon cut of the same boiling range but of the HDO / ISO component type.

[0108] According to one embodiment, the biologically derived component obtained by a kraft process comprises, relative to the total mass of the biologically derived component obtained by a kraft process: - 5 to 40% by mass, preferably 5 to 25% by mass, of compounds having 11 to 13 carbon atoms, - 3 to 25% by mass, preferably 5 to 20% by mass, of compounds having 14 to 16 carbon atoms, - 20 to 65% by mass, preferably 30 to 60% by mass, of compounds having 17 to 18 carbon atoms, and - 3 to 20% by mass, preferably 5 to 15% by mass, of compounds having 19 and 20 carbon atoms.

[0109] According to one embodiment, the biologically derived component from a kraft process comprises, relative to the total mass of the biologically derived component from a kraft process: - 2 to 15% by mass of compounds having 11 carbon atoms, - 2 to 15% by mass of compounds having 12 carbon atoms, - 2 to 15% by mass of compounds having 13 carbon atoms, - 2 to 15% by mass of compounds having 14 carbon atoms, - 2 to 15% by mass of compounds having 15 carbon atoms, - 2 to 15% by mass of compounds having 16 carbon atoms, - 5 to 25% by mass of compounds having 17 carbon atoms, - 15 to 60% by mass of compounds having 18 carbon atoms, - 2 to 25% by mass of compounds having 19 carbon atoms, - 2 to 15% by mass of compounds having 20 carbon atoms.

[0110] According to one embodiment, the hydrocarbon filler used in the process of the invention comprises 100% of component(s) of biological origin from a kraft process, as defined in the present invention.

[0111] According to another embodiment, the hydrocarbon charge comprises, or even consists of: - 30 to 90% by mass, preferably 40 to 70% by mass, of a component of biological origin produced using a kraft process, and - 10 to 70% by mass, preferably 30 to 60% by mass, of a component of biological origin obtained through a hydrodeoxygenation and hydroisomerization process of a vegetable or animal oil,

[0112] in relation to the total mass of the hydrocarbon charge.

[0113] The inventors have indeed discovered that this combination of components of biological origin makes it possible to improve the lifespan of the hydrogenation catalyst while maintaining good properties for the naphthenic fluid from the hydrogenation process.

[0114] The biologically derived component obtained from a hydrodeoxygenation and hydroisomerization process of a vegetable or animal oil – hereinafter also referred to as the HDO / ISO component – ​​may include, for example: - at least 90% by mass of isoparaffins, - less than 25% by mass of n-paraffins, - less than 1% by mass of aromatics, and - less than 5% naphthenes by mass,

[0115] compared to the total mass of the biological component obtained from a hydrodeoxygenation and hydroisomerization process of a vegetable or animal oil.

[0116] Preferably, the ratio between the mass proportion of isoparaffins and the mass proportion of n-paraffins in the biologically derived component from a hydrodeoxygenation and hydroisomerization process of a vegetable or animal oil ranges from 1.5 to 11, preferably from 2 to 10.

[0117] The HDO / ISO component possibly implemented in the invention comprises a content of at least 75% by mass of isoparaffins, preferably at least 80% by mass, more preferably at least 90% by mass of isoparaffins, or even at least 95% by mass, relative to the total mass of the HDO / ISO component.

[0118] The HDO / ISO component possibly implemented in the invention comprises a content of less than or equal to 25% by mass of n-paraffins, preferably less than or equal to 20% by mass, preferably even less than or equal to 10% by mass of n-paraffins, or even less than or equal to 5% by mass, relative to the total mass of the HDO / ISO component.

[0119] Preferably, the HDO / ISO component possibly implemented in the invention has an isoparaffins to n-paraffins mass ratio of at least 4:1, preferably at least 9:1, preferably even at least 12:1, preferably at least 15:1, or even at least 19:1.

[0120] Preferably, the HDO / ISO component possibly implemented in the invention comprises, relative to the total mass of the HDO / ISO component, a mass content of naphthenic compounds less than or equal to 1%, preferably less than or equal to 0.5% and more preferably less than or equal to 100 ppm.

[0121] Preferably, the HDO / ISO component possibly implemented in the invention comprises, relative to the total mass of the HDO / ISO component, a mass content of aromatic compounds less than or equal to 1%, preferably less than or equal to 0.5% and more preferably less than or equal to 100 ppm.

[0122] According to one embodiment, the HDO / ISO component possibly implemented in the invention comprises at least 80% by mass of isoparaffins, less than 20% by mass of n-paraffins, less than 1% by mass of naphthenes and less than 1% by mass of aromatics, relative to the total mass of the HDO / ISO component.

[0123] According to one embodiment, the HDO / ISO component possibly implemented in the invention comprises, relative to the total mass of the HDO / ISO component, a mass content of isoparaffins ranging from 90 to 100% and a mass content of n-paraffins ranging from 0 to 10%, preferably from 95 to 100% isoparaffins and from 0 to 5% n-paraffins and more preferably from 98% to 100% isoparaffins and from 0 to 2% n-paraffins.

[0124] According to a preferred embodiment, the HDO / ISO component possibly implemented in the invention comprises a mass content of isoparaffins ranging from 90 to 100%, a mass content of n-paraffins ranging from 0 to 10% and a mass content of naphthenes less than or equal to 1%, relative to the total mass of the HDO / ISO component.

[0125] Preferably the HDO / ISO component possibly implemented in the invention comprises a mass content of 95 to 100% isoparaffins, a mass content of 0 to 5% n-paraffins and a mass content of less than or equal to 0.5% naphthenes, relative to the total mass of the HDO / ISO component.

[0126] Preferably the HDO / ISO component possibly implemented in the invention comprises a mass content of 95 to 100% isoparaffins, a mass content of 0 to 5% n-paraffins and a mass content of less than or equal to 0.5% aromatic compounds, relative to the total mass of the HDO / ISO component.

[0127] According to a preferred embodiment, the HDO / ISO component optionally implemented in the invention comprises an isoparaffins mass content of 90 to 100%, an n-paraffins mass content of 0 to 10%, a naphthenes mass content of 1% or less, and an aromatics mass content of 1% or less. Preferably, the HDO / ISO component implemented according to the invention comprises an isoparaffins mass content of 95 to 100%, n-paraffins mass content of 0 to 5%, a naphthenes mass content of 0.5% or less, and an aromatics mass content of 0.5% or less. Preferably also the HDO / ISO component possibly implemented in the invention comprises a mass content of 95 to 100% isoparaffins, 0 to 5% n-paraffins and a mass content of aromatic compounds less than or equal to 100 ppm.

[0128] According to one embodiment, the HDO / ISO component possibly implemented in the invention has a biological carbon content of at least 90% by mass, preferably at least 95% by mass, and even more preferably at least 97% by mass, relative to the total mass of carbon atoms in the HDO / ISO component.

[0129] According to one embodiment, the HDO / ISO component possibly implemented in the invention comprises at least 80% by mass of isoparaffins, less than 20% by mass of n-paraffins, less than 1% by mass of naphthenes and less than 0.5% by mass of aromatics, relative to the total mass of the HDO / ISO component and has a biogenic carbon content of at least 90% by mass relative to the total mass of carbon atoms of the HDO / ISO component.

[0130] According to one embodiment, the HDO / ISO component possibly implemented in the invention comprises at least 90% by mass of isoparaffins, less than 10% by mass of n-paraffins, less than 1% by mass of naphthenes and less than 0.5% by mass of aromatics, relative to the total mass of the HDO / ISO component and has a biogenic carbon content of at least 90% by mass relative to the total mass of carbon atoms of the HDO / ISO component.

[0131] The HDO / ISO component possibly implemented in the invention also preferably has an extremely low mass content of sulfur compounds, typically less than or equal to 5 ppm, preferably less than or equal to 3 ppm and more preferably less than or equal to 0.5 ppm at a level too low to be detected by conventional low-sulfur analyzers.

[0132] The HDO / ISO component possibly implemented in the invention also preferably has a flash point greater than or equal to 80°C, preferably greater than or equal to 110°C, preferably greater than or equal to 120°C and more preferably greater than or equal to 140°C according to ASTM D93. A high flash point, typically greater than 110°C, makes it possible in particular to overcome safety problems during storage and transport while avoiding excessive flammability of the HDO / ISO component.

[0133] The HDO / ISO component possibly implemented in the invention also preferably has a vapor pressure at 20°C less than or equal to 0.01kPa.

[0134] According to one embodiment, the HDO / ISO component possibly implemented in the invention also preferably has a flash point greater than or equal to 110°C according to ASTM D93 and a vapor pressure at 20°C less than or equal to 0.01kPa.

[0135] Preferably the HDO / ISO component possibly implemented in the invention has a flash point greater than or equal to 120°C and a vapor pressure at 20°C less than or equal to 0.01kPa.

[0136] And more preferably, the HDO / ISO component possibly implemented in the invention has a flash point greater than or equal to 140°C and a vapor pressure at 20°C less than or equal to 0.01kPa.

[0137] The HDO / ISO component possibly implemented in the invention also preferably has a kinematic viscosity at 40°C less than or equal to 5 cSt, preferably less than or equal to 4 cSt, measured according to ASTM D445.

[0138] Preferably, the HDO / ISO component possibly implemented in the invention has an initial boiling point and a final boiling point in the range of 200 to 400°C, preferably from 240 to 350°C, preferably again from 250 to 340°C.

[0139] Boiling points can be determined according to ASTM D86.

[0140] According to one embodiment, the HDO / ISO component possibly implemented in the invention comprises, relative to the total mass of the HDO / ISO component: - 20 to 80% by mass of C15 isoparaffins and 20 to 80% by mass of C16 isoparaffins, said fluid possibly comprising isoparaffins having 14 carbon atoms or fewer and / or isoparaffins having 17 carbon atoms or more; or - 3 to 20% by mass of C15 isoparaffins, 20 to 70% by mass of C16 isoparaffins, 5 to 40% by mass of C17 isoparaffins, and 5 to 40% by mass of C18 isoparaffins, said fluid possibly comprising isoparaffins having 14 carbon atoms or fewer and / or isoparaffins having 19 carbon atoms or more; or - 5 to 40% by mass of C17 isoparaffins and 60 to 95% by mass of C18 isoparaffins, said fluid possibly comprising isoparaffins having 16 or fewer carbon atoms and / or isoparaffins having 19 or more carbon atoms.

[0141] According to a particular embodiment, the HDO / ISO component implemented according to the invention comprises, relative to the total mass of the HDO / ISO component: - 30 to 60% by mass of C15 isoparaffins and 30 to 60% by mass of C16 isoparaffins, said fluid being able to comprise isoparaffins having 14 carbon atoms or fewer and / or isoparaffins having 17 carbon atoms or more; or - 5 to 15% by mass of C15 isoparaffins, 30 to 60% by mass of C16 isoparaffins, 10 to 30% by mass of C17 isoparaffins, and 10 to 30% by mass of C18 isoparaffins, said fluid possibly comprising isoparaffins having 14 carbon atoms or fewer and / or isoparaffins having 19 carbon atoms or more; or - 10 to 30% by mass of C17 isoparaffins and 60 to 90% by mass of C18 isoparaffins, said fluid possibly comprising isoparaffins having 16 carbon atoms or less and / or isoparaffins having 19 carbon atoms or more.

[0142] The expression "CX isoparaffins" refers to isoparaffins comprising X carbon atoms.

[0143] The HDO / ISO component possibly implemented in the invention typically exhibits a biodegradability of at least 60% at 28 days, measured according to OECD 301B standard. Thus, typically, the HDO / ISO component according to the invention will be said to be "easily biodegradable" or "readily biodegradable" in English.

[0144] In contrast, a product will be said to be "inherently biodegradable" if it has a biodegradability ranging from 20 to less than 60% at 28 days according to OECD standard 301, for example according to OECD standard 301B.

[0145] Preferably, the HDO / ISO component implemented according to the invention has a biodegradability of at least 60% at 28 days, measured according to OECD standard 306. OECD standard 306 is more stringent than OECD standard 301B. Process for obtaining the HDO / ISO component:

[0146] The HDO / ISO component optionally implemented in the invention can be obtained as follows. The HDO / ISO component implemented according to the invention is a hydrocarbon fraction typically obtained from the conversion of biomass from vegetable or animal oil type, also including animal fats and fish oils.

[0147] Preferably, the HDO / ISO component is obtained by a process comprising hydrodeoxygenation (HDO) and isomerization (ISO) steps. The hydrodeoxygenation (HDO) step leads to the decomposition of the structures of the biological esters or triglyceride constituents, the removal of oxygenated, phosphorus, and sulfur compounds, and the hydrogenation of the olefinic bonds. The product of the hydrodeoxygenation reaction is then isomerized. A fractionation step may preferably follow the hydrodeoxygenation and isomerization steps. Advantageously, the fractions of interest are then subjected to hydrotreating and distillation steps to obtain the desired HDO / ISO component specifications.

[0148] This HDO / ISO process is carried out on a raw biological feedstock, also called biomass or biological feedstock, selected from the group consisting of vegetable oils, animal fats, fish oils, and mixtures thereof. Suitable biological feedstocks include, for example, rapeseed oil, canola oil, talloil, sunflower oil, soybean oil, hemp oil, olive oil, linseed oil, mustard oil, palm oil, peanut oil, castor oil, coconut oil, animal fats such as tallow, recycled food fats, genetically engineered feedstocks, and biological feedstocks produced from microorganisms such as algae and bacteria. Condensation products, esters, or other derivatives obtained from raw biological materials can also be used as feedstocks.

[0149] Preferably, the biologically derived raw material is an ester or a triglyceride derivative. This material is first subjected to a hydrodeoxygenation (HDO) step to break down the structure of the constituent esters or triglycerides and eliminate oxygenated, phosphorus, and sulfur compounds concomitantly with the hydrogenation of the olefinic bonds. This hydrodeoxygenation (HDO) step of the biologically derived raw material is followed by isomerization of the resulting product, leading to branching of the hydrocarbon chain and improved properties of the paraffin at low temperatures.

[0150] Methods for obtaining the HDO / ISO component that can be implemented in the invention are described in applications WO2014 / 033762, EP2084245 or EP2368967.

[0151] According to this second embodiment, which uses a mixture of a component from a kraft process and an HDO / ISO component, the hydrocarbon filler may preferably comprise: - 3 to 30% by mass, preferably 5 to 20% by mass, of compounds having 11 to 13 carbon atoms, - 10 to 35% by mass, preferably 15 to 30% by mass, of compounds having 14 to 16 carbon atoms, - 30 to 55% by mass, preferably 35 to 50% by mass, of compounds having 17 to 18 carbon atoms, and - 3 to 20% by mass, preferably 5 to 15% by mass, of compounds having 19 and 20 carbon atoms.

[0152] in relation to the total mass of the hydrocarbon charge. Hydrogenation process

[0153] The process of the invention includes a hydrogenation step, typically catalytic, of a hydrocarbon feedstock, as defined in the invention.

[0154] Preferably, the hydrogenation step is a catalytic hydrogenation step at a temperature of 80 to 180°C and at a pressure of 50 to 160 bar.

[0155] The hydrogen used in the hydrogenation unit is typically highly purified hydrogen. Highly purified means hydrogen with a purity, for example, greater than 99%, although other grades may also be used.

[0156] The hydrogenation step is typically carried out using catalysts. Typical hydrogenation catalysts can be either bulk or supported and may include the following metals: nickel, platinum, palladium, rhenium, rhodium, nickel tungstate, nickel-molybdenum, molybdenum, and cobalt-molybdenum. The supports may be silica, alumina, silica-alumina, or zeolites.

[0157] A preferred catalyst is a nickel-based catalyst on an alumina support with a specific surface area preferably ranging from 100 to 200 m² / g of catalyst, or a nickel-based bulk catalyst. The hydrogenation conditions are typically as follows: - Pressure: 50 to 160 bars, preferably 80 to 150 bars and more preferably 100 to 140 bars; - Temperature: 80 to 180 °C, preferably 120 to 160 °C and more preferably 150 to 160 °C; - Hourly volumetric speed (WH): 0.2 to 5 hr ', preferably 0.4 to 3 hr 1 and more preferably 0.5 to 1.5 hr *.

[0158] The hydrogen treatment rate can be adapted to the conditions mentioned above (temperature, pressure and WH) and can go up to 200 Nm3 / tonne of charge to be treated.

[0159] The temperature in the reactors is typically between 150 and 160°C with a pressure of 100 to 140 bar while the hourly volumetric velocity is approximately 1 hr 1 with a treatment rate adapted according to the quality of the load to be treated and the parameters of the first hydrogenation reactor.

[0160] Hydrogenation can take place in one or more reactors in series. The reactors can include one or more catalytic beds. The catalytic beds are generally fixed catalytic beds.

[0161] The hydrogenation process preferably comprises two or three reactors, preferably three reactors and is more preferably carried out in three reactors in series.

[0162] The first reactor traps sulfur compounds and hydrogenates essentially all unsaturated compounds and up to approximately 90% by weight of aromatic compounds. The product from the first reactor contains substantially no sulfur compounds. In the second stage, i.e., in the second reactor, the hydrogenation of aromatics continues, and up to 99% by weight of the aromatics are thus hydrogenated.

[0163] The third stage in the third reactor is a finishing stage enabling aromatics levels to be obtained below 100 ppm, preferably below 50 ppm, preferably below 20 ppm.

[0164] It is possible to use a reactor which has two or three or more catalytic beds. The catalysts can be present in varying or essentially equal quantities in each reactor; for three reactors, the quantities as a function of weight can for example be 0.05-0.5 / 0.10-0.70 / 0.25-0.85, preferably 0.07-0.25 / 0.15-0.35 / 0.4-0.78 and more preferably 0.10-0.20 / 0.20-0.32 / 0.48-0.70.

[0165] It is also possible to use one or two hydrogenation reactors instead of three.

[0166] It is also possible that the first reactor is composed of twin reactors operated alternately. This mode of operation allows, in particular, for easier loading and unloading of the catalysts: when the first reactor contains the saturated catalyst first (substantially all the sulfur is trapped on and / or in the catalyst), it must be changed frequently.

[0167] A single reactor may also be used in which two, three or more catalytic beds are installed.

[0168] It may be necessary to insert quench boxes (in the English sense of "reaction quenching") into the recycle system or between reactors to cool the effluents from one reactor to another or from one catalytic bed to another in order to control the temperatures and hydrothermal balance of each reaction. According to a preferred embodiment, there are no cooling or quenching intermediates.

[0169] According to one embodiment, the product from the process and / or the separated gases are at least partially recycled into the feed system of the hydrogenation reactors. This dilution helps to maintain the exothermicity of the reaction within controlled limits, particularly in the first stage. Recycling also allows for heat exchange before the reaction and better temperature control.

[0170] The effluent from the hydrogenation unit contains mainly the hydrogenated product and hydrogen. Flash separators are used to separate the effluent into the gaseous phase, mainly residual hydrogen, and the liquid phase, mainly hydrogenated hydrocarbon fractions. The process can be carried out using three flash separators: one at high pressure, one at intermediate pressure, and one at low pressure very close to atmospheric pressure.

[0171] The gaseous hydrogen that is collected at the top of the flash separators can be recycled into the feed system of the hydrogenation unit or at different levels in the hydrogenation units between the reactors.

[0172] Advantageously, the hydrogenation step is carried out until a hydrogenated hydrocarbon feed with a very low aromatic content is obtained, preferably less than 500 ppm by mass, preferably less than 300 ppm by mass and more preferably less than 100 ppm by mass.

[0173] The hydrogenated hydrocarbon feedstock has an aromatics content that is lower than the aromatics content of the feedstock (before the hydrogenation step). Advantageously, the hydrogenation is carried out under the conditions mentioned above until an aromatics conversion rate of between 95 and 100%, preferably between 98 and 99.99%, is obtained.

[0174] Hydrogenation allows the transformation of aromatic compounds into naphthenic compounds.

[0175] The hydrogenation step can be followed by a measurement of the aromatic content by UV spectrometry or high-performance liquid chromatography (HPLC). HPLC is preferably used when the amount of aromatics is greater than 0.1% by mass, but the samples can also be diluted so that the aromatic content can be measured by UV spectrometry when the aromatic content of the samples is too high.

[0176] Distillation, also called fractionation, can be carried out before the hydrogenation step and / or after the hydrogenation step, preferably after the hydrogenation step.

[0177] According to one embodiment, the distillation step is carried out at a temperature ranging from 60 to 180°C and at a pressure ranging from 50 to 1000 mbars.

[0178] Preferably, the distillation step is implemented so as to obtain at the end of the distillation one or more hydrocarbon cuts each having a boiling range narrower than the boiling range of the hydrocarbon feed at the inlet of the distillation.

[0179] According to one embodiment, the boiling range of the hydrocarbon fractions after distillation is less than or equal to 100°C, preferably less than or equal to 80°C, and preferably less than or equal to 70°C. According to another embodiment, the boiling range of the hydrocarbon fractions obtained from distillation is from 10 to 100°C, preferably from 15 to 80°C, and preferably from 20 to 70°C.

[0180] According to one embodiment, at least two hydrocarbon cuts or even at least three hydrocarbon cuts are obtained at the end of the distillation according to the invention, these hydrocarbon cuts having different boiling ranges, the width of the boiling ranges being able to be identical or different between the different cuts.

[0181] According to one embodiment, the distillation is carried out in such a way that it is possible to simultaneously remove various hydrocarbon cuts from the distillation column and that their boiling temperature can be predetermined.

[0182] By adapting the feed through its initial and final boiling points, the hydrogenation reactors, separators, and distillation unit can be directly connected without the need for intermediate tanks. This integration of hydrogenation and distillation allows for optimized thermal integration, a reduction in the number of devices, and energy savings.

[0183] The naphthenic fluid obtained by the process of the invention typically comprises:

[0184] a) a biocarbon content greater than or equal to 90% by mass relative to the total mass of carbon atoms in the naphthenic fluid,

[0185] b) a naphthene content ranging from 6 to 50% by mass, relative to the total mass of the naphthenic fluid,

[0186] c) a non-cyclic paraffin content ranging from 50 to 90% by mass, relative to the total mass of the naphthenic fluid,

[0187] d) an aromatics content less than or equal to 500 ppm by mass, relative to the total mass of the naphthenic fluid.

[0188] Preferably, the naphthenic fluid obtained by the process of the invention has an aromatics content of less than or equal to 500 ppm by mass, preferably less than or equal to 300 ppm by mass, preferably even less than or equal to 100 ppm by mass, relative to the total mass of the naphthenic fluid.

[0189] Preferably, the naphthenic fluid obtained by the process of the invention has a distillation range of less than 100°C, advantageously ranging from 10 to 80°C.

[0190] By way of example, the process of the invention can lead, after possible distillation, to one or more of the following naphthenic cuts: - a section (naphthenic fluid) characterized by the following boiling points: initial point -170°C, - a section (naphthenic fluid) characterized by the following boiling points: 170°C-230°C, - a cut (naphthenic fluid) characterized by the following boiling points: 230°C-275, - a section (naphthenic fluid) characterized by the following boiling points: 275°C-315°C, - a cut (naphthenic fluid) characterized by the following boiling points: 315-end point.

[0191] According to one embodiment, the naphthenic fluid obtained by the process of the invention comprises:

[0192] a) a biocarbon content greater than or equal to 95% by mass relative to the total mass of carbon atoms in the naphthenic fluid,

[0193] b) a naphthene content ranging from 20 to 50% by mass, relative to the total mass of the naphthenic fluid,

[0194] c) a non-cyclic paraffin content ranging from 50 to 75% by mass, relative to the total mass of the naphthenic fluid,

[0195] d) an aromatics content of less than or equal to 100 ppm by mass, relative to the total mass of the naphthenic fluid,

[0196] preferably the isoparaffins / n-paraffins mass ratio of the naphthenic fluid ranges from 1 to 8, preferably from 1.5 to 4.

[0197] This embodiment is typically obtained when the hydrocarbon filler comprises 100% of a component of biological origin from a kraft process.

[0198] According to one embodiment, the naphthenic fluid obtained by the process of the invention comprises:

[0199] a) a biocarbon content greater than or equal to 95% by mass relative to the total mass of carbon atoms in the naphthenic fluid,

[0200] b) a naphthene content ranging from 6 to 40% by mass, relative to the total mass of the naphthenic fluid,

[0201] c) a non-cyclic paraffin content ranging from 60 to 90% by mass, relative to the total mass of the naphthenic fluid,

[0202] d) an aromatics content of less than or equal to 100 ppm by mass, relative to the total mass of the naphthenic fluid,

[0203] preferably the isoparaffins / n-paraffins mass ratio of the naphthenic fluid ranges from 1.5 to 11, preferably from 2 to 10.

[0204] This embodiment is typically obtained when the hydrocarbon filler comprises a mixture of a biological component obtained from a kraft process and an HDO / ISO compound as defined in the present invention. Naphthenic fluid

[0205] The invention also relates to a naphthenic fluid as such, as well as to a naphthenic fluid obtainable by the process of the invention. The naphthenic fluid is also referred to as a naphthenic cut in the context of the present invention.

[0206] The naphthenic fluid according to the invention comprises:

[0207] a) a biocarbon content greater than or equal to 90% by mass relative to the total mass of carbon atoms in the naphthenic fluid,

[0208] b) a naphthene content ranging from 6 to 50% by mass, relative to the total mass of the naphthenic fluid,

[0209] c) a non-cyclic paraffin content ranging from 50 to 90% by mass, relative to the total mass of the naphthenic fluid,

[0210] d) an aromatics content less than or equal to 500 ppm by mass, relative to the total mass of the naphthenic fluid.

[0211] Preferably, the naphthenic fluid according to the invention has an aromatics content of less than or equal to 500 ppm by mass, preferably less than or equal to 300 ppm by mass, preferably even less than or equal to 100 ppm by mass, relative to the total mass of the naphthenic fluid.

[0212] Preferably, the naphthenic fluid according to the invention has a distillation range of less than 100°C, advantageously ranging from 10 to 80°C.

[0213] Advantageously, the naphthenic fluid has an initial boiling point and a final boiling point in the range of 130 to 400°C and a boiling range (difference between the final boiling point and the initial boiling point) of 10 to 80°C.

[0214] According to one embodiment, the naphthenic fluid according to the invention has all of the following characteristics:

[0215] a) a biocarbon content greater than or equal to 95% by mass relative to the total mass of carbon atoms in the naphthenic fluid,

[0216] b) a naphthene content ranging from 6 to 50% by mass, relative to the total mass of the naphthenic fluid,

[0217] c) a non-cyclic paraffin content ranging from 50 to 90% by mass, relative to the total mass of the naphthenic fluid,

[0218] d) an aromatics content of less than or equal to 300 ppm by mass, relative to the total mass of the naphthenic fluid,

[0219] e) an initial boiling point and a final boiling point in the range of 130 to 400°C and a boiling range of 10 to 80°C.

[0220] According to one embodiment, the naphthenic fluid according to the invention is selected from: - a fluid comprising 80 to 98% by mass of compounds having 10 to 13 carbon atoms, relative to the total mass of the fluid, or - a fluid comprising 80 to 98% by mass of compounds having 10 to 13 carbon atoms, relative to the total mass of the fluid, or - a fluid having an initial and final boiling point in the range of 200 to 300°C and comprising 55 to 80% by mass of compounds having 15 to 17 carbon atoms, relative to the total mass of the fluid, or - a fluid comprising 80 to 99% by mass of compounds having 16 to 18 carbon atoms, relative to the total mass of the fluid, or - a fluid having an initial boiling point of at least 300°C and comprising 20 to 45% by mass of compounds having 19 to 20 carbon atoms, relative to the total mass of the fluid.

[0221] According to one embodiment, the naphthenic fluid according to the invention comprises:

[0222] a) a biocarbon content greater than or equal to 95% by mass relative to the total mass of carbon atoms in the naphthenic fluid,

[0223] b) a naphthene content ranging from 20 to 50% by mass, relative to the total mass of the naphthenic fluid,

[0224] c) a non-cyclic paraffin content ranging from 50 to 75% by mass, relative to the total mass of the naphthenic fluid,

[0225] d) an aromatics content of less than or equal to 100 ppm by mass, relative to the total mass of the naphthenic fluid,

[0226] preferably the isoparaffins / n-paraffins mass ratio of the naphthenic fluid ranges from 1 to 8, preferably from 1.5 to 4.

[0227] According to one embodiment, the naphthenic fluid according to the invention comprises:

[0228] a) a biocarbon content greater than or equal to 95% by mass relative to the total mass of carbon atoms in the naphthenic fluid,

[0229] b) a naphthene content ranging from 6 to 40% by mass, relative to the total mass of the naphthenic fluid,

[0230] c) a non-cyclic paraffin content ranging from 60 to 90% by mass, relative to the total mass of the naphthenic fluid,

[0231] d) an aromatics content of less than or equal to 100 ppm by mass, relative to the total mass of the naphthenic fluid,

[0232] preferably the isoparaffins / n-paraffins mass ratio of the naphthenic fluid ranges from 1.5 to 11, preferably from 2 to 10.

[0233] According to one embodiment, the boiling range of the fractions according to the invention is less than or equal to 100°C, preferably less than or equal to 80°C, and more preferably less than or equal to 70°C. According to another embodiment, the boiling range of the hydrocarbon fractions according to the invention is from 10 to 100°C, preferably from 15 to 80°C, and more preferably from 20 to 70°C. Use of naphthenic fluid

[0234] The invention further relates to the use of the naphthenic fluid according to the invention or obtained according to the process of the invention as a drilling fluid or as a solvent or as a thermal fluid or as an additive in fuel formulation, for example as a solvent for the chemical industry, as an extraction solvent, as a solvent in an ink formulation, in a resin formulation, in an adhesive formulation, in a paint composition, for coating material (e.g. wood), for treating material (e.g. wood), for polymerization, aerosol, cleaning or water treatment, as an oil for sealants.

[0235] Naphthenic fluids according to the invention or obtained according to the invention can be used: as drilling fluids, in hydraulic fracturing, in mining, in water treatment, as industrial solvents, in the composition of paints, for decorative coatings, in coating fluids, in the automotive industry, in the textile industry, in metal extraction, in explosives, in oil dispersants, in concrete release formulations, in adhesives, in printing inks, in metalworking fluids, in coating fluids, in rolling oils, particularly for aluminum, as cutting fluids, as rolling oils, as electrical discharge machining (EDM) fluids, as rust inhibitors, as industrial lubricants, as thinning oils, in sealants such as mastics or polymers, particularly silicone-based,as viscosity reducers in plasticized polyvinyl chloride formulations, in resins, in varnishes, in polymers used in water treatment, papermaking or printing pulps, particularly as thickeners, cleaning and / or degreasing solvents, for suspension polymerization, in the food processing industry, for food-grade applications, home care, heat transfer media, shock absorbers, insulating oils, hydraulic oils, gear oils, turbine oils, textile oils and transmission fluids such as automatic transmission fluids or, formulations for manual gearboxes, and as solvents in chemical reactions, including crystallization, extraction and fermentation, as a dielectric fluid or coolant. EXAMPLES

[0236] In the remainder of this description, examples are given by way of illustration of the present invention and are not intended in any way to limit its scope.

[0237] Example 1: Description of hydrocarbon charges

[0238] Table 1 lists the physicochemical properties of two charges hydrocarbons.

[0239] The CH1 hydrocarbon filler is a component of biological origin obtained from a kraft process as defined in the present invention.

[0240] The CH2 hydrocarbon filler comprises, in relation to the total mass of the CH2 filler, 50% by mass of CH1 and 50% by mass of an HDO / ISO component as defined in the present invention.

[0241] [Tables 1] Characteristics CH1 CH2 Aromatics (% by mass) 7 3.5% Isoparaffins (% by mass) 44 69.5% n-paraffins (% by mass) 21 13% Naphthenic (% by mass) 28 14 C9 (% by mass) 1.11 1.1 C1O (% by mass) 4.75 2.3 C1I (% by mass) 5.04 3.0 C12 (% by mass) 3.77 3.2 C13 (% by mass) 3.34 2.7 C14 (% by mass) 3.54 3.0 C15 (% by mass) 3.55 6.3 C16 (% by mass) 6.41 14.9 C17 (% by mass) 12.62 15.2 Cl8 (% by mass) 43.16 27.8 C19 (% by mass) 5.33 8.0 C20 (% by mass) 2.37 3.3 C21 (% by mass) 0.78 1.0 C22 (% by mass) 0.72 1.0 Amount of carbon from biological sources (%) 100 100 Initial boiling point IBP (°C) 172.6 174 Final boiling point FBP (°C) 351.5 351 OECD biodegradability (28 days) (%) >60% >60% Density at 15°C (kg / m3) 817.9 788.9 Viscosity at 40°C (cSt) 3.35 2.43

[0242] The following standards and methods were used to measure the above properties: - density at 15°C: ASTM D4052;

[0243] - viscosity at 40°C: ASTM D445 - Boiling point: ASTM D86; - biodegradability: OECD method 306;

[0244] - Carbon of biological origin: ASTM D 6866 standard, the sample being prepared for this test according to the ASTM D7026 standard. Example 2#: hydrogenation

[0245] The hydrocarbon feedstock CH1 of Table 1 was hydrogenated in the presence of a nickel-based catalyst on an alumina support with a specific surface area ranging from 100 to 200 m² / g of catalyst. The following hydrogenation conditions were implemented:

[0246] - Temperature: 150°C

[0247] - pressure: 100 bar

[0248] - WH: 1 h 1

[0249] Hydrogenation is continued until an aromatics content of less than 100 ppm is obtained. The aromatics content can be measured by UV spectrometry.

[0250] The hydrogenated CH1 hydrocarbon feedstock is then distilled to give naphthenic fluids NI, N2, N3 and N4 described in Table 2.

[0251] [Tableaux2] Standard NI N2 N3 N4 Density at 15° C (kg / m3) ASTM D405 2,798.5 820.4 806.6 843.3 Kinematic viscosity at 40°C (cSt) ASTM D445 1.2 2.4 3.9 9.1 Flash point (closed cup) (°C) ASTM D93 42 97 138 164 Aniline point ASTM D611 93.7 98.2 Initial boiling point IB P (°C) ASTM D86 148.6 226.1 278.1 306.3 Final boiling point FBP (°C) ASTM D86 221.5 271.7 300.3 387.6

[0252] The CH2 hydrocarbon feedstock from Table 1 was hydrogenated in the presence of a nickel-based catalyst on an alumina support with a specific surface area ranging from 100 to 200 m² / g of catalyst. The following hydrogenation conditions were implemented:

[0253] - Temperature: 150°C

[0254] - pressure: 100 bar

[0255] - WH: 1 h 1

[0256] Hydrogenation is continued until an aromatics content of less than 20 ppm is obtained. The aromatics content can be measured by UV spectrometry.

[0257] The hydrogenated CH2 hydrocarbon feedstock is then distilled to give naphthenic fluids N5, N6, N7 and N8 described in Table 3. The N8 cut is a 308°C+ cut and corresponds to the bottom cut after distillation of the N7 cut.

[0258] [Tables3] Standard N5 N6 N7 N8 Density at 15°C (kg / m3) ASTM D405 2 794.1 791.8 791.6 823.5 Kinematic viscosity at 40°C (cSt) ASTM D445 1.3 2.4 3.45 7.0 Flash point (closed cup) (°C) ASTM D93 60 104.5 138.0 162.0 Aniline point ASTM D611 69.6 88.5 96.2 nd Initial boiling point IB P(°C) ASTM D86 177.3 233.1 272.7 nd Final boiling point FBP (°C) ASTM D86 225.7 269.4 293.3 nd Pour point (°C) ASTM D97 -60 -27 0

[0259] nd means "not determined".

[0260] The N5 fluid (type cut 170-230°C) is particularly well suited for coating, aerosol and cleaning applications.

[0261] The N6 fluid (cut type 230-275°C) is particularly well suited for drilling, water treatment, solvent applications for ink formulation.

[0262] The N7 fluid (cut type 275-308°C) is particularly well suited for drilling, hydraulic fracturing, and mining applications.

[0263] The N8 fluid (type cut 308+°C) is particularly well suited for coolant, plant protection, cosmetic, sealant and lubricant applications.

[0264] The inventors further observed that the catalyst life was improved with the CH2 feed compared to the CH1 feed. Indeed, the addition of an HDO / ISO component to the feed improves the hydrogenation catalyst life.

Claims

Demands

1. A process for preparing a naphthenic fluid, said process comprising a step of hydrogenating a hydrocarbon feed comprising: - 5 to 40% by mass of naphthenes, - 50 to 90% by mass of non-cyclic paraffins, and - 1 to 10% by mass of aromatic compounds, relative to the total mass of the hydrocarbon feed, said hydrocarbon feed having a biocarbon content greater than or equal to 90% by mass, relative to the total mass of carbon in the hydrocarbon feed.

2. A process according to claim 1, wherein the hydrocarbon feed comprises at least 70% by mass, preferably 100% by mass, of one or more components of biological origin, relative to the total mass of the hydrocarbon feed, at least one component of biological origin being preferably from a kraft process.

3. A process according to claim 2, wherein the biological component obtained by a kraft process comprises: - 20 to 40% by mass of naphthenes, - 50 to 75% by mass of non-cyclic paraffins, and - 4 to 10% by mass of aromatic compounds, relative to the total mass of the biological component obtained by a kraft process, preferably the isoparaffins / n-paraffins mass ratio of the biological component obtained by a kraft process ranges from 1 to 8, preferably from 1.5 to 4.

4. A process according to any one of claims 1 to 3, wherein the hydrocarbon feedstock has one or more of the following characteristics: - a naphthene content of 10 to 35% by mass relative to the total mass of the hydrocarbon feedstock, and / or - a non-cyclic paraffin content of 60 to 90% by mass relative to the total mass of the hydrocarbon feedstock, and / or - an aromatic compound content of 2 to 10% by mass relative to the total mass of the hydrocarbon feed, and / or - a biocarbon content greater than or equal to 95% by mass relative to the total carbon mass of the hydrocarbon feed, and / or - an initial boiling point in the range of 50 to 250°C, preferably 100 to 200°C, and / or - an end boiling point in the range of 150 to 400°C, preferably 200 to 390°C, and / or - a boiling range with a width greater than or equal to 50°C, preferably greater than or equal to 100°C, and / or - a kinematic viscosity at 40°C less than or equal to 10 cSt, preferably less than or equal to 5 cSt.

5. A process according to any one of claims 1 to 4, wherein the naphthenic fluid has an aromatics content of less than or equal to 500 ppm by mass, preferably less than or equal to 300 ppm by mass, preferably even less than or equal to 100 ppm by mass, relative to the total mass of the naphthenic fluid.

6. A process according to any one of claims 1 to 5, further comprising a distillation step carried out before and / or after the hydrogenation step.

7. A process according to any one of claims 1 to 6, wherein the hydrocarbon filler comprises an isoparaffins / n-paraffins mass ratio of 1 to 11, preferably from 1.5 to 10.

8. A process according to any one of claims 1 to 7, wherein the hydrocarbon filler comprises, or even consists of: - 30 to 90% by mass, preferably 40 to 70% by mass, of a biological component obtained from a kraft process, and - 10 to 70% by mass, preferably 30 to 60% by mass, of a biological component obtained from a hydrodeoxygenation and hydroisomerization process of a vegetable or animal oil, relative to the total mass of the hydrocarbon load.

9. A process according to claim 8, wherein the biological component obtained from a hydrodeoxygenation and hydroisomerization process of a vegetable or animal oil comprises: - at least 75% by mass of isoparaffins, - less than 25% by mass of n-paraffins, - less than 1% by mass of aromatics, and - less than 1% by mass of naphthenes, relative to the total mass of the biological component obtained from a hydrodeoxygenation and hydroisomerization process of a vegetable or animal oil, preferably the isoparaffins / n-paraffins mass ratio of the biological component obtained from a hydrodeoxygenation and hydroisomerization process of a vegetable or animal oil ranges from 1.5 to 11, preferably from 2 to 10.

10. A process according to any one of claims 1 to 7, wherein the hydrocarbon feedstock comprises 100% by mass of a biological component obtained from a kraft process.

11. Naphthenic fluid comprising: a) a biocarbon content greater than or equal to 90% by mass relative to the total mass of carbon atoms in the naphthenic fluid, b) a naphthenes content ranging from 6 to 50% by mass relative to the total mass of the naphthenic fluid, c) a non-cyclic paraffins content ranging from 50 to 90% by mass relative to the total mass of the naphthenic fluid, d) an aromatics content less than or equal to 500 ppm by mass relative to the total mass of the naphthenic fluid.

12. Naphthenic fluid according to claim 12, wherein the aromatics content is less than or equal to 500 ppm by mass, preferably less than or equal to 300 ppm by mass, preferably even less than or equal to 100 ppm by mass, relative to the total mass of the naphthenic fluid.

13. Naphthenic fluid according to claim 11 or 12, comprising: a) a biocarbon content greater than or equal to 95% by mass relative to the total mass of carbon atoms in the naphthenic fluid, b) a naphthenes content of 20 to 50% by mass, relative to the total mass of the naphthenic fluid, c) a non-cyclic paraffins content of 50 to 75% by mass, relative to the total mass of the naphthenic fluid, d) an aromatics content of less than or equal to 100 ppm by mass, relative to the total mass of the naphthenic fluid, preferably the isoparaffins / n-paraffins mass ratio of the naphthenic fluid ranges from 1 to 8, preferably from 1.5 to 4.

14. Naphthenic fluid according to claim 11 or 12, comprising: a) a biocarbon content greater than or equal to 95% by mass relative to the total mass of carbon atoms in the naphthenic fluid, b) a naphthenes content of 6 to 40% by mass relative to the total mass of the naphthenic fluid, c) a non-cyclic paraffins content of 60 to 90% by mass relative to the total mass of the naphthenic fluid, d) an aromatics content less than or equal to 100 ppm by mass relative to the total mass of the naphthenic fluid, preferably the isoparaffins / n-paraffins mass ratio of the naphthenic fluid of 1.5 to 11, preferably 2 to 10.

15. Use of a naphthenic fluid obtained according to the process of any one of claims 1 to 10 or of a naphthenic fluid according to any one of claims 11 to 14, as a drilling fluid, as a solvent, in particular for ink, paint, resin, adhesive, as an oil for sealants, as a thermal fluid or as an additive in fuel formulation, preferably as an oil for sealants and / or as a solvent for ink, paint, resin and / or adhesive.