Process for producing fluids from pyrolysis oil derived from plastic recovery

Abstract

The invention is a process for preparing a fluid having a boiling range below 100 DEG C, said process comprising:-a step of catalytically hydrogenating a pyrolysis oil at a temperature of from 100 DEG C to 220 DEG C and a pressure of from 20 bar to 150 bar, based on the total weight of the pyrolysis oil, said pyrolysis oil comprising:-700 ppm to 3000 ppm by weight of aromatic compounds,-40% to 50% by weight of n-paraffin compounds,-1% by weight of an aromatic compound,-1% by weight of an aromatic compound,-1% by weight of an aromatic compound,-1% by weight of an aromatic compound,-1% by weight of an aromatic compound,-1% by weight of an aromatic compound,-1% by weight of an aromatic compound The present invention relates to a fluid comprising-40 to 50 wt% of an isoparaffin compound, and-2 to 15 wt% of a cycloparaffin compound, the fluid comprising less than 700 ppm by weight of aromatic compounds, based on the total weight of the fluid.

Description

Field of the Invention

[0001] The present invention relates to a method for producing a fluid with a low aromatic compound content meeting the requirements of the pharmacopoeia from a raw material which is a hydrotreated pyrolysis oil derived from plastic recycling. Background Art

[0002] Considering environmental issues, recycling plastic waste has become an inevitable step in the life cycle of plastics.

[0003] The industry is seeking to recycle and add value to plastics to give them a second life.

[0004] Plastics are usually made of polymers, and the first conversion of plastics can produce pyrolysis oil.

[0005] Pyrolysis oil usually contains a relatively high content of aromatic hydrocarbons.

[0006] One object of the present invention is to provide a method for preparing a fluid which contains less than 300 ppm by weight of aromatic compounds and 25 - 43% by weight of n - alkanes, meets the requirements of the pharmacopoeia, and the fluid is from the feed of the chemical recycling of plastic waste.

[0007] Another object of the present invention is to provide an alkane fluid meeting the requirements of the pharmacopoeia, especially the requirements of the French and European Pharmacopoeias. Summary of the Invention

[0008] The present invention relates to a method for preparing a fluid with a boiling range below 100 °C, the method comprising:

[0009] - a step of catalytically hydrogenating pyrolysis oil at a temperature of 100 °C to 220 °C and a pressure of 20 bar to 150 bar,

[0010] Based on the total weight of the pyrolysis oil, the pyrolysis oil contains:

[0011] - 700 ppm to 3000 ppm by weight of aromatic compounds,

[0012] - 40% to 50% by weight of n - alkane compounds,

[0013] - 40% to 50% by weight of iso - alkane compounds, and

[0014] - 2% to 15% by weight of cycloalkane compounds,

[0015] Based on the total weight of the fluid, the fluid contains less than 700 ppm by weight of aromatic compounds.

[0016] Preferably, based on the total weight of the pyrolysis oil, the pyrolysis oil contains:

[0017] - 42 wt% to 48 wt% of n-alkane compounds, and

[0018] - 42 wt% to 48 wt% of iso-alkane compounds, and

[0019] - 5 wt% to 10 wt% of cycloalkane compounds.

[0020] According to one embodiment, the weight ratio of iso-alkanes to n-alkanes in the pyrolysis oil is in the range of 0.5 to 1.5.

[0021] Preferably, based on the total weight of the pyrolysis oil, the aromatic compound content of the pyrolysis oil is 900 to 2800 ppm, preferably 1000 to 2700 ppm of aromatic compounds.

[0022] According to one embodiment of the present invention, the catalytic hydrogenation is carried out in the presence of a catalyst selected from nickel, nickel tungstate, nickel molybdenum alloy, molybdenum, cobalt molybdate, nickel molybdate supported on a silica and / or alumina support or zeolite, preferably a nickel-based catalyst preferably supported on a silica and / or alumina support.

[0023] According to one embodiment of the present invention, the method includes a preliminary step of preparing pyrolysis oil by a method including at least one depolymerization step performed on plastic waste.

[0024] Preferably, the plastic waste is selected from polyolefins, polypropylene, polyethylene, and polystyrene.

[0025] According to one embodiment of the present invention, the method further includes a fractionation step performed before and / or after the catalytic hydrogenation step to provide at least one fraction having a boiling range lower than 100 °C.

[0026] Preferably, the fractionation step is performed after the catalytic hydrogenation step to obtain at least one fluid selected from:

[0027] - A fluid having an end boiling point in the range of 100 °C to 180 °C, preferably 120 °C to 170 °C,

[0028] - A fluid having an end boiling point greater than 180 °C and at most 240 °C, preferably 190 °C to 230 °C, and

[0029] - A fluid having an end boiling point greater than 240 °C and at most 300 °C, preferably 250 to 280 °C.

[0030] The present invention also relates to a fluid having a boiling range lower than 100 °C and having an initial boiling point and an end boiling point of 50 °C to 350 °C, and based on the total weight of the fluid, the fluid comprises:

[0031] - 23 wt% to 63 wt% of n-alkane compounds, and

[0032] - 33 wt% to 63 wt% of an isoparaffinic compound, and

[0033] - 2 wt% to 15 wt% of a naphthenic compound, and

[0034] - aromatic compounds less than 700 ppm by weight.

[0035] According to one embodiment, the fluid of the present invention can be obtained by the method according to the present invention.

[0036] Preferably, the fluid contains aromatic compounds less than 300 ppm by weight, preferably less than 20 ppm by weight.

[0037] According to one embodiment, the weight ratio of isoparaffin / n - paraffin of the fluid of the present invention is 1 / 2 to 3 / 1.

[0038] Preferably, the fluid of the present invention is selected from:

[0039] - a fluid having an initial boiling point of 30 °C to 90 °C and a final boiling point of 100 °C to 180 °C,

[0040] - a fluid having an initial boiling point of 100 °C to 180 °C and a final boiling point greater than 190 °C and at most 240 °C, and

[0041] - a fluid having an initial boiling point of 200 °C to 270 °C and a final boiling point greater than 240 °C and at most 300 °C,

[0042] Preferably selected from:

[0043] - a fluid having an initial boiling point of 30 °C to 70 °C and a final boiling point of 120 °C to 170 °C,

[0044] - a fluid having an initial boiling point of 120 °C to 180 °C and a final boiling point of 190 °C to 230 °C,

[0045] - a fluid having an initial boiling point of 200 °C to 240 °C and a final boiling point of 245 °C to 270 °C, and

[0046] - a fluid having an initial boiling point of 240 °C to 260 °C and a final boiling point of 260 °C to 270 °C.

[0047] Finally, the present invention also relates to the use of a fluid according to the present invention as a drilling fluid, as an industrial solvent, as a cutting fluid, as a rolling oil, as an electro-discharge machining fluid, as a rust inhibitor in industrial lubricants, as a diluent oil, as a viscosity reducer in formulations based on plasticized polyvinyl chloride, as a crop protection fluid, as white oil, in particular for coating fluids, metal extraction, the mining industry, explosives, release formulations for concrete, adhesives, printing inks, metalworking fluids, silicone-based sealant products or polymer formulations, resins, pharmaceutical products, cosmetic formulations, coating compositions, polymers for water treatment, paper or printing pastes or cleaning solvents.

[0048] The advantage of the present invention is that it allows to provide a fluid from the pyrolysis oil of the chemical recycling of plastics, which further meets the strict requirements of the pharmacopoeia.

[0049] The inventors have surprisingly found that fluids of pharmacopoeia quality can be obtained from the recycling of plastics.

[0050] In particular, the present invention allows to provide a novel fluid which is an alkane fluid comprising isoalkanes (iP) and normal alkanes (nP) in a weight ratio iP / nP preferably of 0.5 to 3, a limited amount of cycloalkanes preferably up to 15% by weight and a small amount of aromatic compounds, said aromatic compounds preferably being less than 700 ppm by weight or even less than 300 ppm by weight.

[0051] In the context of the present invention, unless otherwise specified, the boiling range, the initial boiling point and the final boiling point are determined using the method EN ISO 3405. Detailed Description

[0052] The present invention relates to a process for preparing a fluid having a boiling range below 100 °C, said process comprising:

[0053] - a step of catalytically hydrogenating a hydrocarbon pyrolysis oil at a temperature of 100 °C to 220 °C and a pressure of 20 bar to 150 bar,

[0054] Based on the total weight of the pyrolysis oil, the pyrolysis oil comprises:

[0055] - aromatic compounds in an amount of 700 ppm to 3000 ppm by weight,

[0056] - 40% to 50% by weight of normal alkane compounds,

[0057] - 40% to 50% by weight of isoalkane compounds, and

[0058] - 2% to 15% by weight of cycloalkane compounds,

[0059] Based on the total weight of the fluid, the fluid contains less than 700 ppm by weight of aromatic compounds.

[0060] According to one embodiment, the method further includes a step of preparing hydrocarbon pyrolysis oil, preferably by a method including at least one depolymerization step on plastic waste, which is preferably a plastic polymer.

[0061] Fractionation can be carried out before or after the catalytic hydrogenation step to obtain the desired fractions, which are usually defined by a narrow boiling range. If it is carried out before the catalytic hydrogenation, the pyrolysis oil is fractionated.

[0062] In the context of the present invention, "boiling range" means the difference between the final boiling point and the initial boiling point.

[0063] In the context of the present invention, the initial boiling point is necessarily different from and lower than the final boiling point.

[0064] Pyrolysis oil (also referred to as "feedstock" or "raw material") :

[0065] The pyrolysis oil contains 700 ppm to 3000 ppm by weight of aromatic compounds, preferably 900 ppm to 2800 ppm, more preferably 1000 ppm to 2700 ppm of aromatic compounds.

[0066] For aromatic compounds with a quantity below 350 ppm, the aromatic compound content can be measured by UV spectroscopy, and for aromatic compounds with a quantity above 350 ppm, it can be measured by HPLC (IP391 standard).

[0067] In the context of the present invention, the expression "aromatic compounds" encompasses monoaromatic and polyaromatic compounds.

[0068] According to one embodiment, the feed contains monoaromatic compounds and polyaromatic compounds. According to a specific embodiment, the aromatic compounds in the feed consist of monoaromatic compounds and diaromatic compounds.

[0069] Based on the total weight of the feed, the feed contains 40 wt% to 50 wt% of normal paraffin compounds, preferably 42 to 48 wt% of normal paraffin compounds.

[0070] In the context of the present invention, the expression "normal paraffin compounds" encompasses alkanes having a linear (straight-chain) hydrocarbon chain.

[0071] According to one embodiment, based on the total weight of the feed, the feed contains 40 wt% to 50 wt% of isoparaffin compounds, preferably 42 to 48 wt% of isoparaffin compounds.

[0072] In the context of the present invention, the expression "isoparaffin compounds" encompasses alkanes having a branched hydrocarbon chain.

[0073] According to one embodiment, based on the total weight of the feedstock, the feedstock contains 2% to 15% by weight of naphthenic hydrocarbon compounds, preferably 5% to 10% by weight of naphthenic hydrocarbon compounds.

[0074] Within the meaning of the present invention, the expression "naphthenic hydrocarbon compound" encompasses saturated compounds containing at least one ring, which ring is optionally substituted by one or more alkyl groups containing, for example, 1 to 10 carbon atoms.

[0075] According to a particular embodiment, based on the total weight of the feedstock, the feedstock contains:

[0076] - 40% to 50% by weight of normal paraffin hydrocarbon compounds, preferably 42 to 48% by weight of normal paraffin hydrocarbon compounds, and

[0077] - 40% to 50% by weight of isoparaffin hydrocarbon compounds, preferably 42 to 48% by weight of isoparaffin hydrocarbon compounds, and

[0078] - 2% to 15% by weight of naphthenic hydrocarbon compounds, preferably 5% to 10% by weight of naphthenic hydrocarbon compounds.

[0079] Generally, the weight ratio of isoparaffins to normal paraffins in the feedstock is 0.5 to 1.5.

[0080] The paraffin content and the naphthene content can be determined by gas chromatography.

[0081] According to one embodiment, the initial boiling point and the final boiling point of the feedstock are 50°C to 350°C, preferably 100°C to 320°C.

[0082] The boiling point of the feedstock can be measured according to the EN ISO 3405 standard.

[0083] According to one embodiment, the initial boiling point of the feedstock is 50°C to 200°C, preferably 100°C to 150°C, and / or the final boiling point is 250°C to 350°C, preferably 270°C to 320°C.

[0084] According to one embodiment, the feedstock contains less than 10 ppm by weight of carbonyl groups, preferably less than 5 ppm by weight of carbonyl groups, more preferably less than 1 ppm by weight of carbonyl groups. The carbonyl content can be measured by SMS2894.

[0085] According to one embodiment, the feedstock is substantially free of heteroatoms. In particular, the feedstock generally contains less than 1% by weight of heteroatoms, preferably less than 1000 ppm by weight of heteroatoms, more preferably less than 100 ppm by weight of heteroatoms, and even more preferably less than 10 ppm by weight of heteroatoms.

[0086] Within the meaning of the present invention, "heteroatom" means any atom that is not a carbon atom or a hydrogen atom.

[0087] According to a preferred embodiment, the feedstock is selected from pyrolysis oils, and the pyrolysis oils are selected from oils resulting from the chemical recycling of plastic waste, in particular oils resulting from the depolymerization of plastic waste.

[0088] Among plastics, mention may be made of polyolefins, polypropylene, polyethylene and polystyrene.

[0089] The inventors have surprisingly found that very pure fluids can be obtained from such pyrolysis oils resulting from the chemical recycling of plastic waste.

[0090] Preliminary steps for preparing pyrolysis oil

[0091] According to one embodiment of the method for preparing the fluid of the present invention, the method comprises a preliminary step for preparing pyrolysis oil, which preferably comprises at least one depolymerization step carried out on plastic waste. The pyrolysis oil used in the method of the present invention can be prepared according to the method detailed in document US 9,080,107. Generally, the method for preparing pyrolysis oil comprises a depolymerization step of plastic waste and a hydrotreating step of the depolymerization product to obtain a pyrolysis oil containing 700 ppm to 3000 ppm of aromatic compounds. According to this embodiment, the pyrolysis oil is thus hydrotreated.

[0092] According to a specific embodiment, the method for preparing pyrolysis oil comprises the following steps:

[0093] a) continuously feeding plastic waste into an extruder;

[0094] b) melting the plastic waste in the extruder;

[0095] c) depolymerizing the melt in a pyrolysis reactor;

[0096] d) guiding the depolymerization product vapor into a preliminary separation unit;

[0097] e) separating the vapor in the preliminary separation unit by introducing separation;

[0098] f) hydrotreating the product to obtain a pyrolysis oil containing 700 ppm - 3000 ppm of aromatic compounds;

[0099] g) guiding the hydrotreated fraction into a secondary separation unit.

[0100] According to this embodiment, the pyrolysis oil is thus hydrotreated.

[0101] Preferably, the plastic is selected from polyolefins, polypropylene, polyethylene, and polystyrene. Preferably, the feedstock for hydrogenation is derived from the recycling of a single plastic, such as the recycling of plastic waste composed of polyolefins or the recycling of plastic waste composed of polypropylene or the recycling of plastic waste composed of polyethylene or the recycling of plastic waste composed of polystyrene.

[0102] Hydrogenation step

[0103] The pyrolysis oil as defined above is hydrogenated. Preferably, the hydrogenation step is carried out on the hydrotreated pyrolysis oil. The pyrolysis oil may optionally be pre-fractionated.

[0104] The hydrogen used in the hydrogenation unit is usually high-purity hydrogen, such as a purity greater than 99%, although other grades may also be used.

[0105] According to a specific embodiment, the catalyst consists of nickel as a metal compound.

[0106] The hydrogenation conditions are generally as follows:

[0107] - Pressure: 20 bar to 150 bar, preferably 30 bar to 140 bar, most preferably 40 bar to 120 bar; and / or

[0108] - Temperature: 100 to 220 °C, preferably 110 to 200 °C, most preferably 120 to 180 °C; and / or

[0109] - Liquid hourly space velocity (LHSV): 0.2 to 5 h -1 , preferably 0.4 to 3 h -1 , most preferably 0.5 to 1.5 h -1 ; and / or

[0110] - Hydrogen treatment rate: Adapted to the above conditions, which can be up to 200 Nm 3 / ton of feedstock.

[0111] According to a specific embodiment, the hydrogenation is carried out at a temperature of 130 °C to 180 °C and a pressure of 50 bar to 100 bar.

[0112] This hydrogenation step of the method of the present invention can be carried out in one or more reactors. The reactor may include one or more catalytic beds. The catalytic bed is usually a fixed bed.

[0113] The hydrogenation step of the present invention can be carried out in several stages. There can be two or three stages, preferably three stages, preferably in three separate reactors. The first stage generally operates to hydrogenate up to about 90 wt% of the aromatic compounds present in the pyrolysis oil. In the second stage, the hydrogenation of the aromatic compounds continues, and up to 99 wt% of the aromatic compounds can be hydrogenated. The third stage is a finishing stage, allowing the aromatic compound content to be as low as below 300 ppm by weight, for example below 100 ppm, more preferably below 50 ppm by weight.

[0114] According to a preferred embodiment, the hydrogenation is carried out in three stages, preferably in three separate reactors. These three stages allow for the provision of a fluid with a very low aromatic compound content, where optionally the remaining aromatic compounds consist of monoaromatic compounds.

[0115] Hydrogenation is carried out using a catalyst. Typical hydrogenation catalysts include, but are not limited to: nickel, platinum, palladium, rhenium, rhodium, nickel tungstate, nickel molybdenum alloy, molybdenum, cobalt molybdate, nickel molybdate supported on a silica and / or alumina support or zeolite.

[0116] According to a preferred embodiment, the hydrogenation step is carried out in the presence of a nickel catalyst supported on an alumina support. The preferred catalyst is Ni-based and supported on an alumina support, which has a specific surface area varying between 100 - 200 m 2 / g of catalyst.

[0117] In the case where the hydrogenation is carried out in three reactors, the catalyst can be present in different or substantially equal amounts in each reactor. For example, for the three reactors, according to the weight ratio of the catalyst in reactor 1 / reactor 2 / reactor 3 being 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, most preferably 0.10 - 0.20 / 0.20 - 0.32 / 0.48 - 0.70.

[0118] It is also possible that one of the reactors in which the hydrogenation step is carried out is made of a dual reactor operating alternately in a switching mode. This can be useful for catalyst loading and discharging: since the reactor may contain a catalyst that is first poisoned (substantially all sulfur is trapped in and / or on the catalyst), it should be replaced frequently.

[0119] It may be necessary to insert a quench on the recycle to cool the effluent between the reactors or the catalytic beds to control the reaction temperature and thus control the thermodynamic equilibrium of the hydrogenation reaction. In a preferred embodiment, there is no such intermediate cooling or quenching.

[0120] In the case where 2 or 3 reactors are used in the hydrogenation step, the first reactor will act as a heteroatom trap, such as a sulfur trap and any other contaminants (heteroatoms). Thus, this first reactor will capture substantially all of the sulfur. Consequently, the catalyst will quickly become saturated and can be updated from time to time. When this saturated catalyst cannot be regenerated or rejuvenated, the first reactor is considered a sacrificial reactor, and both its size and catalyst content depend on the catalyst update frequency.

[0121] In one embodiment, at least part of the resulting product and / or the separated gas is recycled to the inlet of the hydrogenation stage. If desired, this dilution helps to maintain the exothermicity of the reaction within controlled limits, especially in the first stage. Recycling also allows for heat exchange before the reaction and can better control the temperature.

[0122] According to one embodiment, the method of the present invention further includes the step of recycling a portion of the hydrotreated pyrolysis oil obtained at the outlet of the hydrogenation step before the hydrogenation step so as to mix with the pyrolysis oil as defined in the present invention.

[0123] Within the meaning of the present invention, the expression "a portion of the hydrotreated pyrolysis oil" means the proportion in the volume of the hydrotreated pyrolysis oil, and "this portion" will not be obtained by any specific treatment or specific separation carried out on this recycling.

[0124] The stream leaving the hydrogenation unit contains hydrogenated products and hydrogen. A flash separator is used to separate the effluent into a gas (mainly residual hydrogen) and a liquid (mainly hydrogenated hydrocarbons). The method can be carried out using three flash separators, one at high pressure, one at medium pressure, and one at low pressure, very close to atmospheric pressure.

[0125] The hydrogen collected at the top of the flash separator can be recycled to the inlet of the hydrogenation unit or to different levels in the hydrogenation unit between the reactors.

[0126] Since the finally separated product is at approximately atmospheric pressure, it can be directly fed to an optional fractionation stage, which is preferably carried out under a vacuum pressure of about 10 - 50 mbar, preferably about 30 mbar.

[0127] Advantageously, the hydrogenation step is carried out under the above conditions until a dearomatized fluid with a very low aromatic compound content is obtained, preferably with an aromatic compound content of less than 300 ppm by weight, preferably less than 100 ppm by weight, more preferably less than 50 ppm by weight, and even more preferably less than 20 ppm by weight.

[0128] The aromatic compound content of the hydrogenated fluid is lower than that of the pyrolysis oil. Advantageously, the hydrogenation is carried out under the above conditions until a conversion of aromatic compounds of 95 to 100%, preferably 98 to 99.99% is obtained.

[0129] After the hydrogenation step, the aromatic compound content can be measured by UV spectroscopy or by high performance liquid chromatography (HPLC). When the amount of aromatic compounds is higher than 0.1% by weight, HPLC is preferably used, or, when the aromatic compound content of the sample is too high, the sample can be diluted so that the aromatic compound content can be measured by UV spectroscopy.

[0130] The hydrogenated product has substantially the same initial boiling point and the same final boiling point as the feed (before hydrogenation), and substantially the same density.

[0131] The optional fractionation stage can be operated so that various hydrocarbon fluids can be withdrawn from the fractionation column simultaneously, and their boiling ranges can be predetermined.

[0132] Thus, fractionation can be carried out on the pyrolysis oil before and / or after hydrogenation or both. Fractionation is usually carried out by distillation.

[0133] Thus, the hydrogenation reactor, the separator and the fractionation unit can be directly connected without having to use intermediate tanks. By adjusting the feed, in particular the initial boiling point and the final boiling point of the feed, the final product with the desired initial boiling point and final boiling point can be produced directly without an intermediate storage tank. In addition, this integration of hydrogenation and fractionation allows optimized thermal integration, reduces the number of equipment and saves energy.

[0134] According to one embodiment, the fractionation step is carried out to obtain at least one hydrocarbon fraction, preferably at least two hydrocarbon fractions, more preferably at least three hydrocarbon fractions (also referred to as "fluids"), the hydrocarbon fractions being selected from:

[0135] - a fraction having a final boiling point of 100 to 180 °C, preferably 120 to 170 °C,

[0136] - a fraction having a final boiling point greater than 180 °C and at most 240 °C, preferably 190 °C to 230 °C, and

[0137] - a fraction having a final boiling point greater than 240 °C and at most 300 °C, preferably 250 to 280 °C.

[0138] According to one embodiment, the fractionation step is carried out to obtain at least one hydrocarbon fraction, preferably at least two hydrocarbon fractions, more preferably at least three hydrocarbon fractions, the hydrocarbon fractions being selected from:

[0139] - a fraction having an initial boiling point of 30 °C to 90 °C and a final boiling point of 100 °C to 180 °C,

[0140] - a fraction having an initial boiling point of 100 °C to 180 °C and a final boiling point greater than 190 °C and at most 240 °C, and

[0141] - A fraction having an initial boiling point of 200 °C to 270 °C and a final boiling point of greater than 240 °C and at most 300 °C.

[0142] According to one embodiment, a fractionation step is carried out to obtain the following hydrocarbon fractions:

[0143] - A fraction having an initial boiling point of 30 °C to 70 °C and a final boiling point of 120 °C to 170 °C,

[0144] - A fraction having an initial boiling point of 120 °C to 180 °C and a final boiling point of 190 °C to 230 °C,

[0145] - A fraction having an initial boiling point of 200 °C to 240 °C and a final boiling point of 245 °C to 270 °C, and

[0146] - A fraction having an initial boiling point of 240 °C to 260 °C and a final boiling point of 260 °C to 270 °C.

[0147] According to one embodiment, the method of the present invention comprises:

[0148] i) A step for preparing pyrolysis oil, which comprises at least one step of depolymerizing plastic waste to provide pyrolysis oil, based on the total weight of the pyrolysis oil, the pyrolysis oil contains 700 ppm to 3000 ppm of aromatic compounds by weight and 40 wt% to 50 wt% of normal alkane compounds;

[0149] ii) Catalytic hydrogenation of the pyrolysis oil at a temperature of 100 °C to 220 °C and a pressure of 20 bar to 150 bar to provide a hydrogenated product, based on the total weight of the hydrogenated product, the hydrogenated product contains less than 300 ppm of aromatic compounds by weight and 23 wt% to 63 wt% of normal alkane compounds;

[0150] iii) Fractionating the hydrogenated product to provide at least one fluid, based on the total weight of the fluid, the fluid contains less than 300 ppm of aromatic compounds by weight and 23% to 63 wt% of normal alkane compounds, and the difference between the final boiling point and the initial boiling point of the fluid is less than 100 °C, preferably 10 to 95 °C,

[0151] wherein step i) is preferably carried out in an inert gas atmosphere and preferably comprises the following steps: continuously feeding plastic waste into an extruder, melting the plastic waste in the extruder to obtain a melt, depolymerizing the melt in a pyrolysis reactor, guiding the depolymerized product vapor to a preliminary separation unit, separating the vapor into fractions in the preliminary separation unit by introducing separation, hydrorefining the obtained fractions, and guiding the hydrorefined fractions to a secondary separation unit.

[0152] According to one embodiment, the method of the present invention comprises:

[0153] i) a step for preparing pyrolysis oil, which comprises at least one step of depolymerizing plastic waste to provide pyrolysis oil, based on the total weight of the pyrolysis oil, the pyrolysis oil contains 700 ppm to 3000 ppm of aromatic compounds by weight and 40 wt% to 50 wt% of n-alkane compounds;

[0154] ii) catalytic hydrogenation of the pyrolysis oil at a temperature of 100 °C to 220 °C and a pressure of 20 bar to 150 bar to provide a hydrogenation product, based on the total weight of the hydrogenation product, the hydrogenation product contains less than 300 ppm of aromatic compounds by weight and 23 wt% to 63 wt% of n-alkane compounds;

[0155] iii) fractionating the hydrogenation product to provide at least two fluids, preferably at least three fluids, based on the total weight of the fluid, each fluid contains less than 300 ppm of aromatic compounds by weight, 23 wt% to 63 wt% of n-alkane compounds and 33 wt% to 63 wt% of iso-alkane compounds, the difference between the final boiling point and the initial boiling point of each fluid is less than 100 °C, the fluids are selected from:

[0156] - a fluid having a final boiling point of 100 to 180 °C, preferably 120 to 170 °C,

[0157] - a fluid having a final boiling point greater than 180 °C and at most 240 °C, preferably 190 °C to 230 °C, and

[0158] - a fluid having a final boiling point greater than 240 °C and at most 300 °C, preferably 250 to 280 °C,

[0159] wherein step i) is preferably carried out in an inert gas atmosphere and preferably comprises the following steps: continuously feeding plastic waste into an extruder, melting the plastic waste in the extruder to obtain a melt, depolymerizing the melt in a pyrolysis reactor, guiding the depolymerization product vapor to a preliminary separation unit, separating the vapor into fractions in the preliminary separation unit by introducing separation, hydrofining the obtained fractions, and guiding the hydrofined fractions to a secondary separation unit.

[0160] According to one embodiment, the method of the present invention comprises:

[0161] i) a step for preparing pyrolysis oil, which comprises at least one step of depolymerizing plastic waste to provide pyrolysis oil, based on the total weight of the pyrolysis oil, the pyrolysis oil contains 700 ppm to 3000 ppm of aromatic compounds by weight and 40 wt% to 50 wt% of n-alkane compounds;

[0162] ii) fractionating the pyrolysis oil to provide at least one pyrolysis oil fraction, the difference between the final boiling point and the initial boiling point of the pyrolysis oil fraction being less than 100 °C, preferably 10 to 95 °C;

[0163] iii) catalytically hydrogenating the pyrolysis oil fraction at a temperature of 100 °C to 220 °C and a pressure of 20 bar to 150 bar to provide a fluid which, based on the total weight of the fluid, contains less than 300 ppm by weight of aromatic compounds and 23% to 63% by weight of n-alkane compounds, the difference between the final boiling point and the initial boiling point of the fluid being less than 100 °C, preferably 10 to 95 °C;

[0164] Optionally vi) further fractionating the fluid obtained at the end of step iii) to reduce the width of the boiling range of the fluid,

[0165] wherein step i) is preferably carried out in an inert gas atmosphere and preferably comprises the steps of: continuously feeding plastic waste into an extruder, melting the plastic waste in the extruder to obtain a melt, depolymerizing the melt in a pyrolysis reactor, guiding the depolymerization product vapour to a preliminary separation unit, separating the vapour into fractions in the preliminary separation unit by introduction of separation, hydrorefining the obtained fractions, and guiding the hydrorefined fractions to a secondary separation unit.

[0166] According to one embodiment, the method of the present invention comprises:

[0167] i) a step for preparing pyrolysis oil, the step comprising at least one step of depolymerizing plastic waste to provide pyrolysis oil which, based on the total weight of the pyrolysis oil, contains 700 ppm to 3000 ppm by weight of aromatic compounds, 42% to 48% by weight of n-alkane compounds, 42% to 48% by weight of iso-alkane compounds and 5% to 10% by weight of cycloalkane compounds;

[0168] ii) catalytically hydrogenating the pyrolysis oil at a temperature of 100 °C to 220 °C and a pressure of 20 bar to 150 bar to provide a hydrogenation product which, based on the total weight of the hydrogenation product, contains less than 300 ppm by weight of aromatic compounds, 23% to 63% by weight of n-alkane compounds, 33% to 63% by weight of iso-alkane compounds and 2% to 15% by weight of cycloalkane compounds;

[0169] iii) fractionating the hydrogenation product to provide at least one fluid which, based on the total weight of the fluid, contains less than 300 ppm by weight of aromatic compounds, 23% to 63% by weight of n-alkane compounds, 33% to 63% by weight of iso-alkane compounds and 2% to 15% by weight of cycloalkane compounds, the difference between the final boiling point and the initial boiling point of the fluid being less than 100 °C, preferably 10 to 95 °C,

[0170] Step i) is preferably carried out in an inert gas atmosphere and preferably comprises the following steps: continuously feeding plastic waste into an extruder, melting the plastic waste in the extruder to obtain a melt, depolymerizing the melt in a pyrolysis reactor, guiding the depolymerization product vapor into a preliminary separation unit, separating the vapor into fractions in the preliminary separation unit by introducing separation, hydrorefining the obtained fractions, and guiding the hydrorefined fractions into a secondary separation unit.

[0171] According to one embodiment, the method of the present invention comprises:

[0172] i) A step for preparing pyrolysis oil, the step comprising at least one step of depolymerizing plastic waste to provide pyrolysis oil, based on the total weight of the pyrolysis oil, the pyrolysis oil comprising 700 ppm to 3000 ppm of aromatic compounds, 42% to 48% by weight of n-alkane compounds, 42% to 48% by weight of iso-alkane compounds, and 5% to 10% by weight of cycloalkane compounds;

[0173] ii) Catalytically hydrogenating the pyrolysis oil at a temperature of 100°C to 220°C and a pressure of 20 bar to 150 bar to provide a hydrogenated product, based on the total weight of the hydrogenated product, the hydrogenated product comprising less than 300 ppm of aromatic compounds, 23% to 63% by weight of n-alkane compounds, 33% to 63% by weight of iso-alkane compounds, and 2% to 15% by weight of cycloalkane compounds;

[0174] iii) Fractionating the hydrogenated product to provide at least two fluids, preferably at least three fluids, based on the total weight of the fluid, each fluid comprising less than 300 ppm of aromatic compounds, 23% to 63% by weight of n-alkane compounds, 33% to 63% by weight of iso-alkane compounds, and 2% to 15% by weight of cycloalkane compounds, the difference between the final boiling point and the initial boiling point of each fluid being less than 100°C, preferably 10°C to 95°C, the fluids being selected from:

[0175] - A fluid having a final boiling point of 100 to 180°C, preferably 120 to 170°C,

[0176] - A fluid having a final boiling point greater than 180°C and at most 240°C, preferably 190°C to 230°C, and

[0177] - A fluid having a final boiling point greater than 240°C and at most 300°C, preferably 250 to 280°C,

[0178] Step i) is preferably carried out in an inert gas atmosphere and preferably includes the following steps: continuously feeding plastic waste into an extruder, melting the plastic waste in the extruder to obtain a melt, depolymerizing the melt in a pyrolysis reactor, guiding the depolymerization product vapor into a preliminary separation unit, separating the vapor into fractions in the preliminary separation unit by introducing separation, hydrorefining the obtained fractions, and guiding the hydrorefined fractions into a secondary separation unit.

[0179] According to one embodiment, the method of the present invention includes:

[0180] i) A step for preparing pyrolysis oil, the step including at least one step of depolymerizing plastic waste to provide pyrolysis oil, based on the total weight of the pyrolysis oil, the pyrolysis oil contains 700 ppm to 3000 ppm of aromatic compounds, 42% to 48% by weight of n-alkane compounds, 42% to 48% by weight of iso-alkane compounds, and 5% to 10% by weight of cycloalkane compounds;

[0181] ii) Fractionating the pyrolysis oil to provide at least one pyrolysis oil fraction, the difference between the final boiling point and the initial boiling point of the pyrolysis oil fraction is less than 100 °C, preferably 10 to 95 °C;

[0182] iii) Catalytically hydrogenating the pyrolysis oil fraction at a temperature of 100 °C to 220 °C and a pressure of 20 bar to 150 bar to provide a fluid, based on the total weight of the fluid, the fluid contains less than 300 ppm of aromatic compounds, 23% to 63% by weight of n-alkane compounds, 33% to 63% by weight of iso-alkane compounds, and 2% to 15% by weight of cycloalkane compounds, the difference between the final boiling point and the initial boiling point of the fluid is less than 100 °C, preferably 10 to 95 °C;

[0183] Optionally, vi) Further fractionating the fluid obtained at the end of step iii) to reduce the width of the boiling range of the fluid,

[0184] Wherein step i) is preferably carried out in an inert gas atmosphere and preferably includes the following steps: continuously feeding plastic waste into an extruder, melting the plastic waste in the extruder to obtain a melt, depolymerizing the melt in a pyrolysis reactor, guiding the depolymerization product vapor into a preliminary separation unit, separating the vapor into fractions in the preliminary separation unit by introducing separation, hydrorefining the obtained fractions, and guiding the hydrorefined fractions into a secondary separation unit.

[0185] According to one embodiment, the method of the present invention includes:

[0186] i) A step for preparing pyrolysis oil in an inert gas atmosphere, the step i) includes:

[0187] a) Continuously feed plastic waste into an extruder;

[0188] b) Melt the plastic waste in the extruder;

[0189] c) Depolymerize the melt in a pyrolysis reactor;

[0190] d) Guide the depolymerization product vapor to a pre-separation unit;

[0191] e) Separate the vapor in the preliminary separation unit by introducing separation;

[0192] f) Hydrotreat to provide pyrolysis oil, which, based on the total weight of the pyrolysis oil, contains 700 ppm to 3000 ppm of aromatic compounds by weight and 40% to 50% by weight of n-alkane compounds;

[0193] g) Guide the hydrotreated fraction to a secondary separation unit,

[0194] ii) Catalytically hydrogenate the pyrolysis oil at a temperature of 100 °C to 220 °C and a pressure of 20 bar to 150 bar to provide a hydrogenated product, which, based on the total weight of the hydrogenated product, contains less than 300 ppm of aromatic compounds by weight and 23% to 63% by weight of n-alkane compounds;

[0195] iii) Fractionate the hydrogenated product to provide at least one fluid, which, based on the total weight of the fluid, contains less than 300 ppm of aromatic compounds by weight and 23% to 63% by weight of n-alkane compounds, and the difference between the final boiling point and the initial boiling point of the fluid is less than 100 °C, preferably 10 to 95 °C.

[0196] According to one embodiment, the method of the present invention includes:

[0197] i) Steps for preparing pyrolysis oil in an inert gas atmosphere, and the step i) includes:

[0198] a) Continuously feed plastic waste into an extruder;

[0199] b) Melt the plastic waste in the extruder;

[0200] c) Depolymerize the melt in a pyrolysis reactor;

[0201] d) Guide the depolymerization product vapor to a pre-separation unit;

[0202] e) Separate the vapor in the preliminary separation unit by introducing separation;

[0203] f) Hydrotreating to provide pyrolysis oil which, based on the total weight of the pyrolysis oil, contains 700 ppm to 3000 ppm by weight of aromatic compounds, 40% to 50% by weight of isoparaffinic compounds, and 2% to 15% by weight of naphthenic compounds;

[0204] g) Directing the hydrotreated fraction to a secondary separation unit,

[0205] ii) Catalytically hydrogenating the pyrolysis oil at a temperature of 100 °C to 220 °C and a pressure of 20 bar to 150 bar to provide a hydrogenated product which, based on the total weight of the hydrogenated product, contains less than 300 ppm by weight of aromatic compounds, 33% to 63% by weight of isoparaffinic compounds, and 2% to 15% by weight of naphthenic compounds;

[0206] iii) Fractionating the hydrogenated product to provide at least one fluid which, based on the total weight of the fluid, contains less than 300 ppm by weight of aromatic compounds, 33% to 63% by weight of isoparaffinic compounds, and 2% to 15% by weight of naphthenic compounds, and the difference between the final boiling point and the initial boiling point of the fluid is less than 100 °C, preferably 10 to 95 °C.

[0207] According to one embodiment, the method of the present invention comprises:

[0208] i) A step for preparing pyrolysis oil in an inert gas atmosphere, and the step i) comprises:

[0209] a) Continuously feeding plastic waste into an extruder;

[0210] b) Melting the plastic waste in the extruder;

[0211] c) Depolymerizing the melt in a pyrolysis reactor;

[0212] d) Directing the depolymerization product vapor to a pre-separation unit;

[0213] e) Separating the vapor in the preliminary separation unit by introducing separation;

[0214] f) Hydrotreating to provide pyrolysis oil which, based on the total weight of the pyrolysis oil, contains 700 ppm to 3000 ppm by weight of aromatic compounds, 40% to 50% by weight of isoparaffinic compounds, and 2% to 15% by weight of naphthenic compounds;

[0215] g) Directing the hydrotreated fraction to a secondary separation unit,

[0216] ii) catalytically hydrogenating the pyrolysis oil at a temperature of 100 °C to 220 °C and a pressure of 20 bar to 150 bar to provide a hydrogenated product, based on the total weight of the hydrogenated product, the hydrogenated product comprising less than 300 ppm by weight of aromatic compounds, 33% to 63% by weight of isoparaffin compounds and 2% to 15% by weight of naphthene compounds;

[0217] iii) fractionating the hydrogenated product to provide at least two fluids, preferably at least three fluids, based on the total weight of the fluids, each fluid comprising less than 300 ppm by weight of aromatic compounds, 33% to 63% by weight of isoparaffin compounds and 2% to 15% by weight of naphthene compounds, the difference between the final boiling point and the initial boiling point of each fluid being less than 100 °C, preferably 10 to 95 °C, the fluids being selected from:

[0218] - a fluid having a final boiling point of 100 to 180 °C, preferably 120 to 170 °C,

[0219] - a fluid having a final boiling point greater than 180 °C and at most 240 °C, preferably 190 °C to 230 °C, and

[0220] - a fluid having a final boiling point greater than 240 °C and at most 300 °C, preferably 250 to 280 °C.

[0221] The fluid of the present invention

[0222] The invention also relates to fluids obtainable by the process of the invention, and to the fluids themselves.

[0223] Accordingly, the invention relates to a fluid which, based on the total weight of the fluid, has a difference between the final boiling point and the initial boiling point of less than 100 °C, an aromatic compound content of less than 700 ppm by weight and a normal paraffin content of 23% to 63% by weight.

[0224] The difference between the final boiling point and the initial boiling point of the fluid of the invention is less than 100 °C, preferably in the range of 10 to 95 °C.

[0225] Preferably, the fluid of the invention has an initial boiling point and a final boiling point in the range of 30 to 350 °C, preferably 50 to 320 °C, more preferably 50 to 300 °C.

[0226] According to one embodiment, the fluid is derived from pyrolysis oil, in particular, the fluid can be obtained by the catalytic hydrogenation step of hydrotreated pyrolysis oil.

[0227] Compared with using fossil oil, using pyrolysis oil to prepare the fluid according to the present invention allows an increase in the content of alkanes, especially n-alkanes, in the fluid, especially when the initial boiling point and the final boiling point of the pyrolysis oil and the fossil oil are comparable. Therefore, the inventors unexpectedly emphasized the impact that the method of using pyrolysis oil can have on the composition of the fluid.

[0228] Preferably, the initial boiling point of the fluid according to the present invention is less than 300 °C, preferably less than 280 °C.

[0229] Preferably, if the initial boiling point is 200 - 300 °C, then based on the total weight of the fluid, the amount of isoalkanes is 33 wt% to 47 wt%, and based on the total weight of the fluid, the amount of n-alkanes is 39 wt% to 63 wt%.

[0230] The inventors have particularly found that the pyrolysis oil source of the fluid allows for obtaining this specific combination of boiling point and isoalkane content.

[0231] According to one embodiment, the fluid according to the present invention has a boiling range below 100 °C and a final boiling point selected from:

[0232] - a final boiling point of 100 to 180 °C, preferably 120 to 170 °C,

[0233] - a final boiling point greater than 180 °C and at most 240 °C, preferably 190 °C to 230 °C, and

[0234] - a final boiling point between greater than 240 °C and at most 300 °C, preferably 250 to 280 °C.

[0235] According to one embodiment, the fluid according to the present invention has a boiling range below 100 °C and an initial boiling point and a final boiling point selected from:

[0236] - an initial boiling point of 30 °C to 90 °C and a final boiling point of 100 °C to 180 °C,

[0237] - an initial boiling point of 100 °C to 180 °C and a final boiling point greater than 190 °C and at most 240 °C, and

[0238] - an initial boiling point of 200 °C to 270 °C and a final boiling point greater than 240 °C and at most 300 °C.

[0239] According to one embodiment, the fluid according to the present invention has a boiling range below 100 °C and an initial boiling point and a final boiling point selected from:

[0240] - an initial boiling point of 30 °C to 70 °C and a final boiling point of 120 °C to 170 °C,

[0241] - an initial boiling point of 120 °C to 180 °C and a final boiling point of 190 °C to 230 °C,

[0242] - The initial boiling point is 200 °C to 240 °C, the final boiling point is 45 °C to 270 °C, and

[0243] - The initial boiling point is 240 °C to 260 °C, the final boiling point is 260 °C to 270 °C.

[0244] The fluid of the present invention contains less than 700 ppm of aromatic compounds by weight, preferably less than 300 ppm of aromatic compounds by weight, preferably less than 100 ppm of aromatic compounds by weight, more preferably less than 50 ppm of aromatic compounds by weight, and even more preferably less than 20 ppm of aromatic compounds by weight.

[0245] Preferably, the fluid of the present invention contains less than 1 ppm of polyaromatic compounds (HAP). In particular, the fluid of the present invention meets the requirements of the European Pharmacopoeia for the HAP content.

[0246] Based on the total weight of the fluid, the fluid of the present invention contains 33% to 63% by weight of isoparaffinic compounds.

[0247] Based on the total weight of the fluid, the fluid of the present invention contains 2% to 15% by weight of naphthenic compounds.

[0248] According to a specific embodiment, based on the total weight of the feed, the fluid contains:

[0249] - 23% to 63% by weight of normal paraffinic compounds, and

[0250] - 33% to 63% by weight of isoparaffinic compounds, and

[0251] - 2% to 15% by weight of naphthenic compounds.

[0252] Preferably, the weight ratio of isoparaffins to normal paraffins in the fluid is 1 / 2 to 3 / 1.

[0253] Preferably, the fluid is substantially free of heteroatoms. In particular, the fluid generally contains less than 1% by weight of heteroatoms, preferably less than 1000 ppm by weight of heteroatoms, more preferably less than 100 ppm by weight of heteroatoms, and even more preferably less than 10 ppm by weight of heteroatoms.

[0254] Preferably, the density of the fluid of the present invention at 15 °C is 0.7000 to 0.8500 g / mL, preferably 0.7200 to 0.8000 g / mL.

[0255] Preferably, the viscosity of the fluid of the present invention at 40 °C is 1.0 to 5.0 mm 2 / s, preferably 1.1 to 2.5 mm 2 / s, more preferably 1.2 to 2.0 mm2 / s.

[0256] According to one embodiment, based on the total weight of the fluid, the fluid comprises the following, preferably consists of:

[0257] - 23 wt% to 63 wt% of n-alkane compounds; and

[0258] - 33 wt% to 63 wt% of iso-alkane compounds; and

[0259] - 2 wt% to 15 wt% of naphthene compounds; and

[0260] - aromatic compounds less than 300 ppm by weight.

[0261] According to one embodiment, based on the total weight of the fluid, the fluid comprises the following, preferably consists of:

[0262] - 23 wt% to 63 wt% of n-alkane compounds; and

[0263] - 33 wt% to 63 wt% of iso-alkane compounds; and

[0264] - 2 wt% to 15 wt% of naphthene compounds; and

[0265] - aromatic compounds less than 100 ppm by weight.

[0266] According to one embodiment, based on the total weight of the fluid, the fluid comprises the following, preferably consists of:

[0267] - 23 wt% to 63 wt% of n-alkane compounds; and

[0268] - 33 wt% to 63 wt% of iso-alkane compounds; and

[0269] - 2 wt% to 15 wt% of naphthene compounds; and

[0270] - aromatic compounds less than 50 ppm by weight; and

[0271] wherein the fluid contains less than 1 ppm by weight of polyaromatic compounds.

[0272] According to one embodiment, based on the total weight of the fluid, the fluid comprises the following, preferably consists of:

[0273] - 23 wt% to 63 wt% of n-alkane compounds; and

[0274] - 33 wt% to 63 wt% of iso-alkane compounds; and

[0275] - 2 wt% to 15 wt% of naphthenic hydrocarbon compounds; and

[0276] - aromatic compounds less than 100 ppm by weight; and

[0277] wherein the fluid contains less than 1 ppm by weight of polyaromatic compounds.

[0278] Preferably, the fluid of the present invention also has an extremely low sulfur content, less than 5 ppm, preferably less than 3 ppm, more preferably less than 0.5 ppm, at a level too low to be detected by conventional analyzers capable of measuring extremely low sulfur content.

[0279] Measured according to ASTM D97 standard, the fluid of the present invention preferably has a pour point of less than -10 °C, preferably less than -20 °C.

[0280] According to one embodiment, based on the total weight of the fluid, the fluid comprises the following, preferably consists of the following:

[0281] - 23 wt% to 63 wt% of normal paraffin hydrocarbon compounds; and

[0282] - 33 wt% to 63 wt% of isoparaffin hydrocarbon compounds; and

[0283] - 2 wt% to 15 wt% of naphthenic hydrocarbon compounds; and

[0284] - aromatic compounds less than 100 ppm by weight,

[0285] The fluid is selected from the following fractions:

[0286] - a fraction having an initial boiling point of 30 °C to 90 °C and a final boiling point within 100 °C to 180 °C,

[0287] - a fraction having an initial boiling point of 100 °C to 180 °C and a final boiling point greater than 190 °C and at most 240 °C, and

[0288] - a fraction having an initial boiling point of 200 °C to 270 °C and a final boiling point greater than 240 °C and at most 300 °C.

[0289] According to one embodiment, based on the total weight of the fluid, the fluid of the present invention comprises the following, preferably consists of the following:

[0290] - 23 wt% to 63 wt% of normal paraffin hydrocarbon compounds; and

[0291] - 33 wt% to 63 wt% of isoparaffin hydrocarbon compounds; and

[0292] - 2 wt% to 15 wt% of naphthenic hydrocarbon compounds; and

[0293] - Aromatic compounds less than 100 ppm by weight,

[0294] The fluid is selected from one of the following fractions:

[0295] - A fraction having an end boiling point of 100 to 180 °C, preferably 120 to 170 °C,

[0296] - A fraction having an end boiling point greater than 180 °C and at most 240 °C, preferably 190 °C to 230 °C, and

[0297] - A fraction having an end boiling point greater than 240 °C and at most 300 °C, preferably 250 to 280 °C.

[0298] According to one embodiment, based on the total weight of the fluid, the fluid comprises the following, preferably consists of:

[0299] - 23 wt% to 63 wt% of n-alkane compounds; and

[0300] - 33 wt% to 63 wt% of iso-alkane compounds; and

[0301] - 2 wt% to 15 wt% of cycloalkane compounds; and

[0302] - Aromatic compounds less than 100 ppm by weight; and

[0303] wherein the fluid contains less than 1 ppm by weight of polyaromatic compounds,

[0304] wherein the fluid is selected from one of the following fractions:

[0305] - A fraction having an initial boiling point of 30 °C to 70 °C and an end boiling point of 120 °C to 170 °C,

[0306] - A fraction having an initial boiling point of 120 °C to 180 °C and an end boiling point of 190 °C to 230 °C,

[0307] - A fraction having an initial boiling point of 200 °C to 240 °C and an end boiling point of 245 °C to 270 °C, and

[0308] - A fraction having an initial boiling point of 240 °C to 260 °C and an end boiling point of 260 °C to 270 °C.

[0309] The present invention also relates to a combination of two or more fluids, each fluid as defined in the present invention. For a combination of fluids according to the present invention, the boiling points of the fluids can be significantly different. As an example, the combination of fluids can be at least two fluids selected from the following:

[0310] - A fluid having an initial boiling point between 30 °C and 70 °C and an end boiling point between 120 °C and 170 °C,

[0311] - A fluid having an initial boiling point of 120°C to 180°C and a final boiling point of 190°C to 230°C,

[0312] - A fluid having an initial boiling point of 200°C to 240°C and a final boiling point of 245°C to 270°C, and

[0313] - A fluid having an initial boiling point of 240°C to 260°C and a final boiling point of 260°C to 270°C.

[0314] Furthermore, the fluid of the present invention has remarkable properties in terms of aniline point or solvent power, molecular weight, vapor pressure, viscosity, specified evaporation conditions of systems important for drying, and specified surface tension.

[0315] The fluid according to the present invention can be used alone or in a mixture as a drilling fluid, as an industrial solvent, as a cutting fluid, as a rolling oil, as an electro-discharge machining fluid, as a rust inhibitor in industrial lubricants, as a diluent oil, as a viscosity reducer in formulations based on plasticized polyvinyl chloride, as a crop protection fluid, as white oil.

[0316] The fluid according to the present invention can also be used alone or in a mixture in coating liquids, metal extraction, the mining industry, explosives, release agents for concrete, adhesives, printing inks, metalworking fluids, silicone-based sealing products or polymer formulations, resins, pharmaceutical products, cosmetic formulations, coating compositions, polymers for water treatment, paper or printing pastes or cleaning solvents.

[0317] The present invention also relates to the use of the fluid according to the present invention as a drilling fluid, as an industrial solvent, as a cutting fluid, as a rolling oil, as an electro-discharge machining fluid, as a rust inhibitor in industrial lubricants, as a diluent oil, as a viscosity reducer in formulations based on plasticized polyvinyl chloride, as a crop protection fluid, as white oil, especially for coating liquids, metal extraction, the mining industry, explosives, release agents for concrete, adhesives, printing inks, metalworking fluids, silicone-based sealing products or polymer formulations, resins, pharmaceutical products, cosmetic formulations, coating compositions, polymers for water treatment, paper or printing pastes or cleaning solvents.

[0318] The present invention also relates to the use of pyrolysis oil obtained by recycling plastic waste for preparing a fluid containing less than 300 ppm aromatic compounds by weight.

[0319] The present invention also relates to the use of pyrolysis oil obtained by recycling plastic waste for preparing a fluid, which, based on the total weight of the fluid, contains less than 300 ppm of aromatic compounds by weight, 23% to 63% by weight of n-alkane compounds, 33% to 63% by weight of iso-alkane compounds, and 2% to 15% by weight of cycloalkane compounds.

[0320] Generally, the fluid is obtained by catalytic hydrogenation of pyrolysis oil.

[0321] The characteristics defined for the method of the present invention and for the fluid of the present invention also apply to the use of the pyrolysis oil of the present invention.

[0322] The following examples illustrate the present invention but do not limit the present invention.

[0323] Examples

[0324] Example 1: Preparation of pyrolysis oil

[0325] The pyrolysis oil used in this example is the pyrolysis oil obtained by depolymerization of plastic waste. Table 1 below shows the characteristics of the pyrolysis oil.

[0326] Table 1

[0327] Standards Pyrolysis oil Initial boiling point Simdist ASTM D2887 59.7℃ 10％ Simdist ASTM D2887 131.8℃ 50％ Simdist ASTM D2887 224℃ 90％ Simdist ASTM D2887 303.1℃ Final boiling point Simdist ASTM D2887 347.1℃ Aromatic content IP 391 2600 ppm Kinematic viscosity at 40 °C ASTM D445 <![CDATA[1,428mm 2 / s]]> Pour point ASTM D97 -24,0℃ Density at 15 °C ASTM D4052 <![CDATA[770,3kg / m 3 > Sulfur content ASTM D 5453 0.1 ppm Carbonyl content SMS*2894 0.3 ppm

[0328] *SMS = Swedish Standard Method

[0329] Elemental analysis of the pyrolysis oil shows that the pyrolysis oil contains less than the detection limit (0.1 ppm) of Cu, Fe, Si, Zn, Al, Sn, Pb, Ca, Na, Ca, Ni, Ag, B, Ba, Mg, Mn, Mo, P, Ti, V, Cr, measured by ASTM D711.

[0330] Analysis of the pyrolysis oil by the UOP 588 standard shows that the pyrolysis oil contains less than 0.1 ppm (below the detection limit) of chlorides.

[0331] Analysis of the pyrolysis oil shows that it contains mono-aromatic compounds and di-aromatic compounds.

[0332] Table 2 shows the composition of the pyrolysis oil obtained by gas chromatography of the pyrolysis oil, expressed in weight %, where:

[0333] -nP represents n-alkane,

[0334] -iP means iso-alkane,

[0335] -N represents cycloalkane, which may include iso-cycloalkane and poly-cycloalkane.

[0336] Table 2: Composition of pyrolysis oil

[0337] nP iP N C7 1.25 0.39 1.08 C8 2.24 2.04 0.78 C9 2.73 10.5 4.39 C10 3.41 1.32 0.60 C11 4.39 7.89 0.64 C12 4.55 1.83 1.09 C13 4.47 8.82 C14 5.75 3.1 C15 5.86 3.11 C16 4.13 3.05 C17 3.39 0.57 C18 2.41 2.77 C19 1.14 C20 0.33

[0338] Example 2: Catalytic hydrogenation

[0339] Hydrogenate the pyrolysis oil detailed in Example 1 under the conditions detailed in Table 3 using a nickel catalyst supported on an alumina support.

[0340] Table 3: Hydrogenation conditions

[0341] 1 2 3 4 Temperature (°C) 130 150 170 150 Pressure (bar) 50 50 50 100 <![CDATA[LHSV(h -1 )]]> 1 1 1 1 H2 / HC (Nl / l) 100 100 100 100

[0342] Carry out the hydrogenation conditions until the content of aromatic compounds is less than 100 ppm by weight. Analyses are also carried out to control the amount of polyaromatic compounds.

[0343] Analysis of the hydrogenation product shows that the product does not contain polyaromatic compounds.

[0344] The hydrogenation product has an initial boiling point of 57 °C and a final boiling point of 344 °C as measured according to ASTM D2887.

[0345] The density of the hydrogenation product at 15 °C is 0.7689 kg / m 3 , as measured according to NF EN ISO 12185 (or ASTM D4052).

[0346] The hydrogenation product is then fractionated by distillation to provide four fluids C1, C2, C3 and C4 detailed in Table 4.

[0347] Table 4: Details of the fluids prepared

[0348] C1 C2 C3 C4 Initial boiling point (°C) 52 146 216 250 Final boiling point (°C) 146 216 257 268 Density at 15 °C (mg / mL) 726 764 783 794 Aromatic content (ppm) <50 <50 <50 <50 Carbon atom number range C6-C9 C9-C11 C11-C14 C13-C16 Isoparaffins (wt%) 62 47 43 35 Normal paraffins (wt%) 23 39 51 62 Naphthenes (wt%) 15 14 3 2

Claims

1. A method for preparing a fluid with a boiling range below 100 °C, the method comprises: - a step of catalytically hydrogenating pyrolysis oil at a temperature of 100 °C to 220 °C and a pressure of 20 bar to 150 bar, Based on the total weight of the pyrolysis oil, the pyrolysis oil contains: - 700 ppm to 3000 ppm of aromatic compounds by weight, - 40 wt% to 50 wt% of n-alkane compounds, - 40 wt% to 50 wt% of iso-alkane compounds, and - 2 wt% to 15 wt% of cycloalkane compounds, Based on the total weight of the fluid, the fluid contains less than 700 ppm of aromatic compounds by weight.

2. The method according to claim 1, wherein, Based on the total weight of the pyrolysis oil, the pyrolysis oil contains: - 42 wt% to 48 wt% of n-alkane compounds, and - 42 wt% to 48 wt% of iso-alkane compounds, and - 5 wt% to 10 wt% of cycloalkane compounds.

3. The method according to claim 1 or 2, wherein, The weight ratio of iso-alkane to n-alkane in the pyrolysis oil is 0.5 to 1.

5.

4. The method according to any one of claims 1 to 3, wherein, Based on the total weight of the pyrolysis oil, the aromatic compound content of the pyrolysis oil is 900 to 2800 ppm, preferably 1000 to 2700 ppm of aromatic compounds.

5. The method according to any one of claims 1 to 4, wherein, The catalytic hydrogenation is carried out in the presence of a catalyst selected from nickel, nickel tungstate, nickel molybdenum alloy, molybdenum, cobalt molybdate, nickel molybdate supported on a silica and / or alumina support or zeolite, preferably a nickel-based catalyst preferably supported on a silica and / or alumina support.

6. The method according to any one of claims 1 to 5, wherein, The method includes a preliminary step of preparing pyrolysis oil by a method including at least one depolymerization step on plastic waste.

7. The method according to claim 6, wherein, The plastic waste is selected from polyolefins, polypropylene, polyethylene and polystyrene.

8. The method according to any one of claims 1 to 7, the method further includes a fractionation step carried out before and / or after the catalytic hydrogenation step to provide at least one fraction with a boiling range below 100 °C.

9. The method according to claim 8, wherein, The fractionation step is carried out after the catalytic hydrogenation step to obtain at least one fluid selected from: - a fluid having a final boiling point of 100 °C to 180 °C, preferably 120 °C to 170 °C, - a fluid having a final boiling point greater than 180 °C and at most 240 °C, preferably 190 °C to 230 °C, and - a fluid having a final boiling point greater than 240 °C and at most 300 °C, preferably 250 to 280 °C.

10. A fluid having a boiling range below 100 °C and an initial boiling point and a final boiling point of 50 °C to 350 °C, based on the total weight of the fluid, the fluid contains: - 23 wt% to 63 wt% of n-alkane compounds, and - 33% to 63% by weight of isoparaffinic compounds, and - 2% to 15% by weight of naphthenic compounds, and - aromatic compounds in an amount less than 700 ppm by weight.

11. The fluid according to claim 10, wherein, the fluid is derived from pyrolysis oil, preferably the fluid can be obtained by a catalytic hydrogenation step of pyrolysis oil, more preferably wherein the fluid can be obtained by the method according to any one of claims 1 to 9.

12. The fluid according to claim 10 or 11, which contains aromatic compounds in an amount less than 300 ppm by weight, preferably less than 20 ppm by weight.

13. The fluid according to any one of claims 10 to 12, wherein the weight ratio of isoparaffin to normal paraffin is from 1 / 2 to 3 / 1.

14. The fluid according to any one of claims 10 to 13, which is selected from: - a fluid having an initial boiling point of 30°C to 90°C and a final boiling point of 100°C to 180°C, - a fluid having an initial boiling point of 100°C to 180°C and a final boiling point greater than 190°C and at most 240°C, and - a fluid having an initial boiling point of 200°C to 270°C and a final boiling point greater than 240°C and at most 300°C, preferably selected from: - a fluid having an initial boiling point of 30°C to 70°C and a final boiling point of 120°C to 170°C, - a fluid having an initial boiling point of 120°C to 180°C and a final boiling point of 190°C to 230°C, - a fluid having an initial boiling point of 200°C to 240°C and a final boiling point of 245°C to 270°C, and - a fluid having an initial boiling point of 240°C to 260°C and a final boiling point of 260°C to 270°C.

15. Use of the fluid according to any one of claims 10 to 14 as a drilling fluid, as an industrial solvent, as a cutting fluid, as a rolling oil, as an electro-discharge machining fluid, as a rust inhibitor in industrial lubricants, as a diluent oil, as a viscosity reducer in formulations based on plasticized polyvinyl chloride, as a crop protection fluid, as white oil, especially for coating fluids, metal extraction, the mining industry, explosives, release formulations for concrete, adhesives, printing inks, metalworking fluids, silicone-based sealant products or polymer formulations, resins, pharmaceutical products, cosmetic formulations, coating compositions, polymers for water treatment, paper or printing pastes or cleaning solvents.