BE1028738A1 - PROCESS AND CHARGE FOR THE PRODUCTION OF HYDROCARBONS - Google Patents

Abstract

A process for producing a cracked product comprising a mixture of hydrocarbons, a thermal cracking charge, a cracking product comprising a mixture of hydrocarbons, and a process for producing polymers using the cracked product are provided.

Description

PROCESS AND CHARGE FOR THE PRODUCTION OF HYDROCARBONS

TECHNICAL FIELD The present invention relates generally to a process for the production of hydrocarbons by thermal cracking. The invention relates in particular, but not exclusively, to a process for the manufacture of a cracking product comprising hydrocarbons by thermal cracking of a feedstock at least partially derived from renewable sources, and preferably using at least a part of said product cracking to produce polymers. STATE OF THE ART This section illustrates general information without admitting any of the techniques described here and representative of the state of the art. Steam cracking is an important process for the production of chemicals from fossil hydrocarbons. Ethylene, propene, 1,3-butadiene, and BTX (benzene, toluene, xylenes) are examples of high-value products from a high-gravity fossil naphtha cracker. Steam cracking is the main source of raw materials for conventional petrochemicals, and in particular for the polymer industry. The main polymers such as polyethylene (PE), polypropylene (PP) and polyethylene terephthalate (PET) are usually obtained from raw materials produced by steam cracking of fossil hydrocarbons. Recently, it has been suggested to replace at least some of the fossil feedstocks traditionally used as feedstock for steam cracking with more sustainable feedstocks from renewable sources to address environmental concerns.

Steam cracking mainly produces hydrocarbons, but CO and CO2, for example, are produced as by-products.

SUMMARY According to a first aspect of the invention, there is provided a process comprising the steps of: a) providing a thermal cracking charge comprising 1 to 100% by weight of renewable isomeric paraffin composition based on the total weight of the charge cracking process, the composition of renewable isomeric paraffins comprising at least 60% by weight of paraffins relative to the total weight of the composition of renewable isomeric paraffins, where from 10 to 95% by weight of said paraffins are isoparaffins, and the ratio of the amount in % by weight of isoparaffins with more than three branches to the amount in % by weight of the total isoparaffins is less than 0.15, and 0 to 99% by weight of fossil naphtha relative to the total weight of the charge of thermal cracking, the sum of the quantities in % by weight of the composition of renewable isomeric paraffins and of the fossil naphtha representing at least 90 % by weight of the total weight of the charge of cracked heat transfer; and b) thermally cracking the thermal cracking charge supplied in step a) to form a cracking product comprising a mixture of hydrocarbons. The total amount of CO, CO2 and C:H2 formed in the cracking step is lower when thermal cracking a thermal cracking feed comprising a composition of renewable isomeric paraffins in which the ratio of the amount in % by weight of of isoparaffins with more than three branches on the total weight % amount of isoparaffins in the renewable isomeric paraffins composition is less than 0.15 compared to the thermal cracking of a thermal cracking charge containing a renewable paraffin composition not meeting that criterion.

In some embodiments, the thermal cracking feed comprises 50 to 100% by weight of renewable isomeric paraffin composition based on the total weight of the thermal cracking feed, and 0 to 50% by weight fossil naphtha based on the weight total thermal cracking load.

In some embodiments, the thermal cracking charge comprises 50-85% by weight renewable isomeric paraffin composition and 15-50% by weight fossil naphtha, preferably 60-85% by weight renewable isomeric paraffin composition and 15 to 40% by weight of fossil naphtha, more preferably 70 to 85% by weight of composition of renewable isomeric paraffins and 15 to 30% by weight of fossil naphtha, relative to the total weight of the thermal cracking charge.

The composition of renewable isomeric paraffins promotes the formation of high value chemicals (ethene, propene, 1,3-butadiene, benzene, toluene and xylenes) in the thermal cracking step compared to thermal cracked fossil naphtha.

This effect becomes more pronounced as the amount in % by weight of the composition of isomeric renewable paraffins in the thermal cracking charge increases and, therefore, a thermal cracking charge comprising at least 50% by weight of the composition of isomeric renewable paraffins is preferable.

Increasing the wt% amount of renewable isomeric paraffin composition increases the wt% amount of renewables in the thermal cracking feedstock and therefore in the cracking product.

In certain embodiments, the sum of the amounts in% by weight of the composition of renewable isomeric paraffins and of the fossil naphtha represents at least 95% by weight, preferably at least 99% by weight, with respect to the total weight of the charge thermal cracking.

Thermal cracking feeds comprising mainly the composition of renewable isomeric paraffins and fossil naphtha are particularly suitable for thermal cracking.

In some embodiments, the ratio of the amount in % by weight of isoparaffins with more than three branches to the amount in % by total weight of isoparaffins in the composition of renewable isomeric paraffins is less than 0.12, preferably less to 0.10, more preferably less than 0.05. Decreasing the ratio of the amount in % by weight of isoparaffins with more than three branches to the amount in % by weight of the total isoparaffins in the composition of renewable isomeric paraffins further decreases the total amount of CO, CO: and C:H2 formed in the thermal cracking step.

In certain embodiments, among the isoparaffins contained in the composition of renewable isomeric paraffins at least 80% by weight, preferably at least 85% by weight, more preferably at least 90% by weight, and even more preferably at least 95% by weight, are in the range of C14 to C18 in the number of carbon atoms. The total amount of CO, CO2 and C2H2 formed in the thermal cracking step is further reduced when thermal cracking a thermal cracking feed comprising the renewable isomeric paraffin composition wherein at least 80% by weight of the isoparaffins of the renewable isomer paraffin composition are in the range of C14-C18 carbon number compared to the thermal cracking of a thermal cracking feed comprising a renewable paraffin composition that does not meet this criterion. The total amount of CO, CO, C2Hz formed during the thermal cracking step decreases further as the percentage by weight of isoparaffins in the C14-C18 range of the number of carbon atoms of the composition of isomeric paraffins renewables increases.

In certain embodiments, of the paraffins contained in the composition of renewable isomeric paraffins, 60 to 95% by weight, preferably 60 to 80% by weight, and more preferably 65 to 70% by weight are isoparaffins. Compositions of renewable isomeric paraffins comprising at least 60% by weight of isoparaffins have good cold properties and good miscibility with fossil naphtha. In certain embodiments, the composition of renewable isomeric paraffins comprises paraffins at least 70% by weight, preferably at least 80% by weight, more preferably at least 90% by weight, even more preferably at least 95% by weight , and even more preferably at least 99% by weight, of the total weight of the composition of renewable isomeric paraffins. The thermal cracking feedstocks comprising the composition of renewable isomeric paraffins having a high paraffin content promote in the thermal cracking step a high yield of C2 and C3 hydrocarbons, such as ethene and propene which are both valuable crackers.

In some embodiments, the fossil naphtha comprises 20-85 wt% paraffins, 0-35 wt% olefins, 10-30 wt% naphthenes, and 0-30 wt% aromatics relative to the total weight of fossil naphtha. In certain embodiments, the % by weight of hydrocarbons in the fossil naphtha is at least 95 % by weight, and preferably at least 99 % by weight, of the total weight of the fossil naphtha.

In certain embodiments, the thermal cracking charge comprises sulfur in an amount of 20 to 300 ppm by weight, preferably 20 to 250 ppm by weight, more preferably 20 to 100 ppm by weight, and even more preferably 50 ppm by weight. at 65 ppm by weight. The thermal cracking charge comprising sulfur further decreases the formation of CO and CO: in the thermal cracking step. Since the composition of renewable isomeric paraffins included in the thermal cracking feedstock already reduces the total amount of CO, CO2 and C2Hz formed in the thermal cracking step, it is not necessary for the cracking feedstock thermic contains large amounts of sulphur. A low sulfur content of the thermal cracking feed yields a low sulfur cracked product. In certain embodiments, step b) is carried out at a coil outlet temperature (COT) chosen between 780°C and 890°C, preferably between 800°C and 860°C, more preferably between 800°C and 840°C, and even more preferably between 800°C and 820°C. A low total amount of CO, COz2 and CzH2 can be obtained by performing the thermal cracking step at a coil outlet temperature (COT) selected from a wide temperature range. The choice of TOC between 800°C and 840°C particularly decreases the total amount of CO, CO: and C2H2 formed during the thermal cracking step. In some embodiments, the thermal cracking performed in step b) is steam cracking.

In certain embodiments, the method comprises the step consisting in c) subjecting at least a part of the cracking product formed in step b) to a purification treatment in order to eliminate at least one of the compounds among CO, COz or C2H2. An advantage of the method according to the first aspect is a reduction in the task of removing CO, CO2, CzH2, or a combination thereof, which allows efficient purification.

In certain embodiments, the method comprises step d) consisting in subjecting at least a part of the cracking product formed in step b), or at least a part of the cracking product subjected to the purification treatment of the step c), or both, to a polymerization treatment to produce polymers. In some embodiments, the polymerization treatment is a catalytic polymerization treatment. In certain embodiments, the polymerization treatment comprises bringing into contact at least a part of the cracking product formed in step b), or at least a part of the cracking product subjected to the purification treatment of the step c),

or both, with a polymerization catalyst, optionally in the presence of molecular hydrogen, to form polymers. The cracking product formed in step b) and optionally purified in step c) is particularly suitable for polymerization due to the low total amount of toxic polymerization catalysts CO, CO: and C2H2 formed in the step of thermal cracking. Furthermore, the polymers formed in step d) are at least partially derived from renewable sources and therefore more sustainable than polymers derived exclusively from fossil sources.

In some embodiments, the method includes providing multiple thermal cracking furnaces and performing step b) in at least one of the multiple thermal cracking furnaces. In some embodiments, the method includes obtaining cracked products from multiple thermal cracking furnaces, and mixing the obtained cracking products to form a combined cracking product, and optionally subjecting at least one part of the cracking product combined with a purification treatment to eliminate at least one compound among CO, CO2 or C2Hz, or with a polymerization treatment to form polymers, or with a purification treatment and the polymerization treatment.

According to a second aspect of the invention, a thermal cracking batch comprising 1 to 100% by weight of isomeric renewable paraffins composition of the total weight of the thermal cracking batch is provided, the renewable isomeric paraffins composition comprising at least 60% by weight of paraffins relative to the total weight of the composition of renewable isomeric paraffins, in which from 10 to 95% by weight of said paraffins are isoparaffins, and the ratio of the % by weight of isoparaffins with more than three branches to the amount total isoparaffins is less than 0.15, and 0 to 99% by weight of fossil naphtha of the total weight of the thermal cracking charge, the sum of the amounts in % by weight of the composition of renewable isomeric paraffins and of the fossil naphtha being at least 90% by weight of the total weight of the thermal cracking charge. When submitting a thermal cracking feed comprising a composition of renewable isomeric paraffins in which the ratio of the quantity in % by weight of isoparaffins with more than three branches to the quantity in % by weight of total isoparaffins in the composition of renewable isomeric paraffins is less than 0.15 to the total amount of CO, CO: and C:2H2 formed is less than that subjected to thermal cracking of a thermal cracking charge comprising a renewable paraffinic composition that does not satisfy this criterion . In some embodiments, the thermal cracking feed comprises 50 to 100% by weight of renewable isomeric paraffin composition based on the total weight of the thermal cracking feed, and 0 to 50% by weight fossil naphtha based on the weight total thermal cracking load. In some embodiments, the thermal cracking charge comprises 50-85% by weight renewable isomeric paraffin composition and 15-50% by weight fossil naphtha, preferably 60-85% by weight renewable isomeric paraffin composition and 15 to 40% by weight of fossil naphtha, more preferably 70 to 85% by weight of composition of renewable isomeric paraffins and 15 to 30% by weight of fossil naphtha relative to the total weight of thermal cracking charge. Thermal cracking feeds comprising at least 50% by weight of the composition of renewable isomeric paraffins promote the formation of high value chemicals (HCVs, i.e. ethene, propene, 1,3-butadiene, benzene , toluene and xylenes) when subjected to thermal cracking and are more durable than thermal cracking batches comprising less than wt% renewable isomeric paraffin compositions.

In certain embodiments, the sum of the amounts in% by weight of the composition of renewable isomeric paraffins and of the fossil naphtha represents at least 95% by weight, and preferably at least 99% by weight, of the total weight of the charge of thermal cracking. In some embodiments, the ratio of the amount in % by weight of isoparaffins with more than three branches to the amount in % by total weight of isoparaffins in the composition of renewable isomeric paraffins is less than 0.12, preferably less to 0.10, more preferably less than 0.05. Decreasing the ratio of the wt% amount of isoparaffins with more than three branches to the total wt% amount of isoparaffins in the renewable isomeric paraffin composition included in the thermal cracking feed further decreases the total amount of CO, CO: and C2Hz formed when thermal cracking charge is subjected to thermal cracking. In certain embodiments, the isoparaffins contained in the composition of renewable isomeric paraffins, at least 80% by weight, preferably at least 85% by weight, preferably at least 90% by weight, and even more preferably at least 95 % by weight, are in the range C14-C18 of the number of carbon atoms. Thermal cracking feeds comprising the isomeric renewable paraffin composition wherein at least 80% by weight of the isoparaffins in the isomeric renewable paraffin composition fall within the range of C14-C18 carbon number further decrease the total amount of CO, CO: and C2H2 formed when the thermal cracking charge is subjected to thermal cracking than when a thermal cracking charge which does not comply with this criterion is subjected. This effect becomes more pronounced as the weight % of isoparaffins in the C14-C18 range of the number of carbon atoms in the composition of renewable isomeric paraffins included in the thermal cracking charge increases.

In certain embodiments, the paraffins contained in the composition of renewable isomeric paraffins represent 60 to 95% by weight, preferably 60 to 80% by weight, and more preferably

65 to 70% by weight are isoparaffins. Compositions of renewable isomeric paraffins comprising at least 60% by weight of isoparaffins have good cold properties and good miscibility with fossil naphtha.

In certain embodiments, the composition of renewable isomeric paraffins comprises paraffins at least 70% by weight, preferably at least 80% by weight, more preferably at least 90% by weight, even more preferably at least 95% by weight , even more preferably at least 99% by weight, of the total weight of the composition of renewable isomeric paraffins. A high paraffin content of the renewable isomeric paraffin composition included in the thermal cracking feed promotes a high yield of C2 and C3 hydrocarbons, such as ethene and propylene, when the thermal cracking feed is thermally cracked .

In some embodiments, the fossil naphtha comprises 20-85 wt% paraffins, 0-35 wt% olefins, 10-30 wt% naphthenes, and 0-30 wt% aromatics relative to the total weight of fossil naphtha. In certain embodiments, the % by weight of hydrocarbons in the fossil naphtha is at least 95% by weight, and preferably at least 99% by weight, based on the total weight of the fossil naphtha.

In some embodiments, the thermal cracking feed comprises sulfur at 20 to 300 ppm by weight, preferably 20 to 250 ppm by weight, more preferably 20 to 100 ppm by weight, and even more preferably 50 to 50 ppm by weight. 65 ppm by weight. The thermal cracking charge comprising sulfur further decreases the formation of CO and CO 2 when the thermal cracking charge is subjected to thermal cracking. Since the composition of renewable isomeric paraffins included in the thermal cracking charge already reduces the total amount of CO, CO2 and C2H2 formed when the thermal cracking charge is subjected to thermal cracking, it is not necessary that this filler contains large amounts of sulphur.

According to a third aspect of the invention, there is provided a cracking product comprising a mixture of hydrocarbons obtainable by a process according to the first aspect, in which the sum of the amounts in % by weight of CO, CO: and C2H2 in the cracked product is less than 1.5% by weight, preferably less than 1.3% by weight, more preferably less than 1.1% by weight, even more preferably less than 0.8% by weight with respect to to the total weight of the cracked product.

According to a fourth aspect of the invention, the use of the cracking product is provided according to the third aspect for the production of polymers, such as polypropylene, polyethylene, or both. In certain embodiments, the cracking product according to the third aspect is used for the production of polymers by a catalytic polymerization treatment. The cracking product of the third aspect is particularly suitable for polymerization due to the low total amount of CO, CO2 and C:H2, which are polymerization catalyst poisons.

According to a fifth aspect of the invention, there is provided an article of manufacture comprising polymers which can be obtained by a method according to the first aspect comprising step d) or comprising subjecting at least a part of a product to cracking combined with a polymerization treatment to form polymers. Said polymers comprised in the article of manufacture are at least partially derived from renewable sources and the article of manufacture is therefore more durable than articles of manufacture comprising polymers derived exclusively from fossil sources.

Various aspects and non-binding embodiments of the present invention have been illustrated in the foregoing. The foregoing embodiments only serve to explain certain aspects or steps that may be used in the practice of the present invention. Certain embodiments can only be presented with reference to certain aspects of the invention. Note that the corresponding embodiments may also apply to other aspects.

BRIEF DESCRIPTION OF THE DRAWINGS Some exemplary embodiments of the invention will be described with reference to the accompanying drawings, in which: Figure 1 shows a schematic drawing of a laboratory scale steam cracking plant used in the examples .

DETAILED DESCRIPTION In the following description, like reference signs designate like elements or steps.

The present invention relates to a method comprising providing a thermal cracking feedstock at least partially derived from renewable sources, namely a thermal cracking feedstock comprising a composition of renewable isomeric paraffins, and thermally cracking said thermal cracking feedstock to forming a cracked product comprising a mixture of hydrocarbons. Furthermore, the present invention relates to the use of the cracked product comprising a mixture of hydrocarbons for the production of polymers.

In this document, a composition of renewable isomeric paraffins means a composition derived from a renewable source or renewable sources and comprising to a large extent paraffins (non-cyclic alkanes), both linear normal paraffins (n-praffins) and branched isoparaffins (i-paraffins). Said isoparaffins can be monobranched i-paraffins, di-branched i-paraffins, tri-branched i-paraffins,

i-paraffins comprising more than three branches, or a combination thereof. Preferably, the isoparaffins are methyl substituted isoparaffins, that is to say isoparaffins whose side chain or side chains, that is to say the branch or branches, are methyl side chains. In theory, the number of branches can be determined from a structural formula by first identifying the longest carbon chain and then calculating the branches attached to the longest carbon chain. However, in practice, the number of side chains (branches) can be determined by any suitable method of analysis, such as the analytical method described in the examples.

It was surprising to find that thermal cracking of renewable paraffinic feeds tends to increase the production of undesirable by-products, in particular the total amount of CO, CO2 and C2H2, compared to the thermal cracking of conventional fossil feeds, in particular the fossil naphtha. This undesirable effect has been shown to be particularly pronounced when thermal cracking mixtures of a renewable paraffinic feedstock component and a fossil feedstock component, such as fossil naphtha. CO and CO2 are polymerization catalyst poisons and therefore cracking products used in a polymerization process should contain no more than 15 ppm by volume, more preferably no more than 0.2 ppm by volume, and even more preferably not more than 0.03 ppm by volume of CO and preferably not more than 10 ppm by volume, such as not more than 0.09 ppm by volume, more preferably not more than 0.1 ppm by volume of CO” . C2H2 can also act as a poison for polymerization catalysts, especially for catalysts in the production of polyethylene. Thus, crackers used in a polymerization process should preferably contain C2H2 at less than 10 ppm by volume, more preferably at less than 2.7 ppm by volume, and even more preferably at less than 1 ppm by volume. Therefore, the task of removing CO, CO: and C2H2 is generally high before cracking products from thermal cracking feeds comprising a renewable paraffinic feed component can be used in a polymerization process.

However, it was surprising to find that the above-described effect of an increased total amount of CO, CO: and C2H2 can be mitigated by selecting or supplying as thermal cracking feed or as a feed component of thermal cracking blended with fossil naphtha a renewable isomeric paraffin composition comprising at least 60% by weight of paraffins of the total weight of the renewable isomeric paraffin composition, wherein from 10 to 95% by weight of said paraffins are isoparaffins, and in wherein the ratio of wt% of isoparaffins with more than three branches to the total wt% amount of isoparaffins is less than 0.15, and thermally cracking said thermal cracking charge. Thermally cracking a thermal cracking charge comprising or consisting of the composition of renewable isomeric paraffins wherein the ratio of the % amount by weight of isoparaffins with more than three branches to the % amount by weight of total isoparaffins is less than 0 ,15 reduces the total amount of CO, CO2 and C2H2 formed, compared to thermal cracking feeds comprising or consisting of a renewable paraffinic component not meeting said criterion. Surprisingly, without being bound by any theory, the ratio of the wt% amount of isoparaffins with more than three branches to the total wt% amount of isoparaffins in the composition of renewable isomeric paraffins seems to be an important factor for control the formation of CO, CO: and CaH2 during the thermal cracking process.

In the present disclosure, the percentage by weight of the paraffins in the composition of isomeric renewable paraffins is determined relative to the total weight of the composition of isomeric renewable paraffins, and the percentages by weight of the isoparaffins (% in total weight of the isoparaffins) and of the normal paraffins in the composition of renewable isomeric paraffins are determined respectively relative to the total weight of the paraffins in the composition of renewable isomeric paraffins.

In addition, in the present disclosure, the percentages by weight of the monobranched isoparaffins, of the isoparaffins, di- and tribranched and of the isoparaffins with more than three branches are determined relative to the total weight of the paraffins in the composition of renewable isomeric paraffins, respectively.

The ratio between the amount in % by weight of isoparaffins with more than three branches and the amount in % by weight of the total isoparaffins is, in the present disclosure, determined on the basis of the respective percentages by weight which are determined with respect to the weight total paraffins in the composition of renewable isomeric paraffins.

It has been found that by further decreasing the ratio of the amount in % by weight of isoparaffins with more than three branches compared to the amount in % by weight of total isoparaffins in the composition of renewable isomeric paraffins, the total amount of CO, CO: and C2H2 formed in the thermal cracking step decreases further.

Accordingly, in some embodiments, the ratio of the amount in % by weight of isoparaffins with more than three branches relative to the amount in % by weight of total isoparaffins of the composition of renewable isomeric paraffins is less than 0 .12, preferably less than 0.10, more preferably less than 0.05. The ratio of the amount in % by weight of isoparaffins with more than three branches to the amount in % by weight of total isoparaffins of the composition of renewable isomeric paraffins can be chosen from approximately 0.14, 0.13, 0, 12, 0.11, 0.10, 0.09, 0.08, 0.07, 0.06, 0.05, 0.04, 0.03, 0.02 and 0.01. In some embodiments, the ratio of the weight % amount of isoparaffins with more than three branches to the total weight % amount of isoparaffins of the renewable isomeric paraffin composition is at least 0.01. Accordingly, the ratio of the amount in % by weight of isoparaffins with more than three branches to the amount in % by weight of total isoparaffins of the composition of renewable isomeric paraffins can be at least 0.01 and less than 0.15, preferably at least 0.01 and less than 0.12, more preferably at least 0.01 and less than 0.10 and even more preferably at least 0.01 and less 0, 05. It has further been found that by providing as the thermal cracking charge a thermal cracking charge comprising 1 to 100% by weight of renewable isomeric paraffin composition based on the total weight of the thermal cracking charge, the isomeric paraffin composition comprising at least 60% by weight of paraffins based on the total weight of the composition of renewable isomeric paraffins, in which from 10 to 95% by weight of said paraffins are isoparaffins, and in which at least 80% by weight of said isoparaffins fall within the range of C14-C18 carbon atoms, and in which the ratio of the amount in % by weight of isoparaffins with more than three branches to the % in total weight of isoparaffins is less than 0.15 , preferably less than 0.12, more preferably less than 0.10, even more preferably less than 0.05, and 0 to 99% by weight of fossil naphtha of the total weight of the charge of cr thermal cracking, the sum of the amounts of % by weight of the renewable isomeric paraffin composition and the fossil naphtha being at least 90% by weight of the total weight of the thermal cracking charge the total amount of CO, CO: and of C2Hz formed in the thermal cracking step compared to thermal cracking feeds comprising or consisting of a renewable paraffinic feed component not meeting these criteria.

When thermal cracking a thermal cracking feed comprising or consisting of the isomeric renewable paraffin composition, wherein the isoparaffins of the isomeric renewable paraffin composition constitute at least 80% by weight in the range C14-C18 of the number of carbon atoms, the total amount of CO, CO: and C2H2 formed is reduced compared to thermal cracking feeds comprising or consisting of a renewable paraffinic feed component containing isoparaffins having a wider distribution in carbon atoms .

It appears, without being bound to any theory, that the distribution of the number of carbon atoms of the isoparaffins in the composition of renewable isomeric paraffins is a factor controlling the formation of CO, CO: and C:H2 during the step thermal cracking.

In the present disclosure, the percentage by weight of isoparaffins in the C14-C18 range of carbon atoms is determined relative to the total weight of isoparaffins in the composition of renewable isomeric paraffins.

Increasing the amount in % by weight of isoparaffins falling within the range C14-C18 of the number of carbon atoms in the composition of renewable isomeric paraffins further decreases the total amount of CO, COz and C:H2 formed. at the thermal cracking stage.

Accordingly, in certain embodiments, the isomeric paraffin composition comprises at least 60% by weight of paraffins relative to the total weight of the composition of renewable isomeric paraffins, where 10 to 95% by weight of said paraffins are isoparaffins, and wherein of said isoparaffins at least 85% by weight, preferably at least 90% by weight, more preferably at least 95% by weight, is in the range of C14-C18 carbon number, and wherein the ratio of the wt% amount of isoparaffins with more than three branches to the total wt% amount of isoparaffins is less than 0.15. The amount in % by weight of isoparaffins of the composition of renewable isomeric paraffins in the range C14-C18 of the number of carbon atoms can be chosen from about 85% by weight, 86% by weight, 87% by weight, 88% by weight, 89% by weight, 90% by weight, 91% by weight, 92% by weight, 93% by weight, 94% by weight, 95% by weight, 96% by weight, 97% by weight, 98% by weight, 99% by weight and 100% by weight.

In certain preferred embodiments, the isomeric paraffin composition comprises at least 60% by weight of paraffins relative to the total weight of the composition of renewable isomeric paraffins, in which 10 to 95% by weight of said paraffins are isoparaffins, and in wherein at least 90 wt% of said isoparaffins are in the range of C14-C18 carbon atoms, and wherein the ratio of the wt% amount of isoparaffins with more than three branches to the wt% amount total isoparaffins is less than 0.12. More preferably, the isomeric paraffin composition comprises at least 60% by weight of paraffins relative to the total weight of the composition of renewable isomeric paraffins, in which 10 to 95% by weight of said paraffins are isoparaffins, and in which at least 95 % by weight of said isoparaffins are in the range C14-C18 of the number of carbon atoms, and the ratio of the quantity in % by weight of the isoparaffins with more than three branches on the quantity in % by weight of the total isoparaffins is lower to 0.10, preferably less than 0.05. By simultaneously decreasing the ratio of the amount in % by weight of isoparaffins with more than three branches to the amount in % by weight of total isoparaffins in the composition of renewable isomeric paraffins and by increasing the amount in % by weight of i -paraffins in the range C14-C18 of the number of carbon atoms in the composition of renewable isomeric paraffins the total amount of CO, CO: and C:H2 formed in the thermal cracking step is particularly low.

Renewable isomeric paraffin compositions comprising at least 60% by weight of isoparaffins have good cold properties and can be stored as such in thermal cracker feed tanks not equipped with heaters at low ambient temperature (0° C or less) without interrupting the cracking process. Good cold properties refer here to a low temperature value of the cloud point. Increasing the amount in % by weight of isoparaffins in the composition of isomeric renewable paraffins improves the miscibility of the composition of isomeric renewable paraffins with fossil naphtha, which is an advantage when the thermal cracking charge comprises less than 100 % by weight of the composition of renewable isomeric paraffins and more than 0 % by weight of fossil naphtha of the total weight of the thermal cracking charge. Accordingly, in certain embodiments, the composition of isomeric renewable paraffins comprises at least 60% by weight of paraffins relative to the total weight of the composition of isomeric renewable paraffins, where, among said paraffins, 60 to 95% by weight, preferably 65 to 93% by weight, more preferably 65 to 90% by weight, are isoparaffins and the ratio between the amount in% by weight of isoparaffins with more than three branches and the amount in% by total weight of isoparaffins is lower at 0.15.

It has been found that the undesirable effect of an increase in the total amount of CO, CO2 and C2H2 previously described can become more pronounced when the % by weight of isoparaffins in a renewable paraffinic feed is high. Therefore, the beneficial effect of a decrease in the total amount of CO, CO2 and C2H2 formed during thermal cracking is particularly important when the composition of renewable isomeric paraffins in which the ratio of the amount in % by weight of isoparaffins with more than three branches on the amount in % by total weight of the isoparaffins is less than 0.15, and in which among the isoparaffins of the composition of renewable isomeric paraffins, preferably at least 80% by weight are in the The C14-C18 carbon number range comprises at least 60% by weight isopraffins of the total weight of the paraffins in the renewable isomeric paraffin composition.

Accordingly, in certain embodiments, the composition of isomeric renewable paraffins comprises at least 60% by weight of paraffins relative to the total weight of the composition of isomeric renewable paraffins, in which, among said paraffins, 60 to 95% by weight , preferably 65-93% by weight, more preferably 65-90% by weight are isoparaffins, and wherein of said isoparaffins, at least 85% by weight are in the range of C14-C18 by the number of carbon atoms, and wherein the ratio of the amount in % by weight of isoparaffins with more than three branches to the amount in % by weight of the total isoparaffins is less than 0.12. Further, in certain embodiments, the renewable isomeric paraffin composition comprises at least 60% by weight of paraffins based on the total weight of the renewable isomeric paraffin composition, wherein, among said paraffins, 60 to 95% by weight , preferably 65-93% by weight, more preferably 65-90% by weight are isoparaffins, and wherein of said isoparaffins, at least 90% by weight are in the range of C14-C18 by the number of carbon atoms , and where the ratio of the amount in% by weight of isoparaffins with more than three branches to the amount in% by weight of the total isoparaffins is less than 0.10, preferably less than 0.05. In certain embodiments, the composition of renewable isomeric paraffins comprises at least 60% by weight of paraffins relative to the total weight of the composition of renewable isomeric paraffins, where 60 to 80% by weight of said paraffins, preferably 65 to 70% by weight are isoparaffins, and where the ratio of the amount in% by weight of isoparaffins with more than three branches to the amount in% by weight of the total isoparaffins is less than 0.15, and where among the isoparaffins of the composition of isomeric renewable paraffins, preferably at least 80% by weight is in the range of C14-C18 carbon number. A composition of renewable isomeric paraffins having a moderate degree of isomerization, for example an amount in % by weight of isoparaffins of 80% by weight or less, or 70% by weight or less, favors in the step of thermal cracking the formation of ethylene, which is a high value thermal cracking product.

As already mentioned, the total amount of CO, CO: and C2Hz formed during thermal cracking can be reduced by decreasing the ratio of the amount in % by weight of isoparaffins with more than three branches to the amount in % by total weight of isoparaffins in the composition of renewable isomeric paraffins. Therefore, it is preferable to use low weight percentages of isoparaffins with more than three branches in the composition of renewable isomeric paraffins. Preferably, the composition of renewable isomeric paraffins comprises isoparaffins with more than three branches at less than 14% by weight, preferably less than 12% by weight, even more preferably less than 10% by weight, even more preferably less than 8 % by weight, even more preferably less than 5% by weight, and even more preferably less than 3% by weight, for example 1% by weight or less, or 0.5% by weight or less, of the total weight of paraffins in the composition of renewable isomeric paraffins. The renewable isomeric paraffin composition may comprise isoparaffins with more than three branches at 1 to 14% by weight, preferably 2 to 12% by weight, preferably 2 to 10% by weight, and more preferably 2 to 5% by weight relative to the total weight of paraffins in the composition of renewable isomeric paraffins. Monobranched isoparaffins, especially monomethyl substituted isoparaffins, promote the formation of propylene, a high-value cracking product, during the thermal cracking step. It is therefore preferable that the composition of renewable isomeric paraffins comprises at least 30% by weight, preferably at least 35% by weight, more preferably at least 40% by weight, more preferably at least 45% by weight, and even more preferably at least 50% by weight of monobranched isoparaffins relative to the total weight of the paraffins in the composition of renewable isomeric paraffins. Optionally, in certain representations, the ratio of the quantity in % by weight of monobranched isoparaffins to the quantity in % by total weight of isoparaffins in the composition of renewable isomeric paraffins is at least 0.3, preferably of at least 0.4, more preferably at least 0.5, even more preferably at least 0.6, even more preferably at least 0.7 and even more preferably at least 0.8. Since the isoparaffins of the renewable isomeric paraffin composition are either monobranched isoparaffins, di- and tri-branched isoparaffins, iso-paraffins with more than three branches, or a combination thereof, the remainder of the isoparaffins consists of the di- and tri-branched isoparaffins . In other words, isoparaffins of the Renewable Isomeric Paraffin composition that are neither monobranched isoparaffins nor isoparaffins with more than three branches are di- and tri-branched isoparaffins.

The renewable isomeric paraffin composition preferably has a high paraffin content. A high paraffin content promotes a high yield of C2 and C3 hydrocarbons, such as ethene and propene, which are both high-value cracked products, in the thermal cracking step. Accordingly, in certain embodiments, the renewable isomeric paraffin composition comprises at least 70% by weight, preferably at least 80% by weight, more preferably at least 90% by weight, even more preferably at least 95% by weight of paraffins relative to the total weight of the composition of renewable isomeric paraffins, where 10 to 95% by weight of said paraffins are isoparaffins and where the ratio of the amount in% by weight of the isoparaffins with more than three branches to that of the isoparaffins is less than 0.15. The amount in % by weight of paraffins in the composition of renewable isomeric paraffins can be chosen from approximately 65% by weight, 70% by weight, 75% by weight, 80% by weight, 85% by weight, 90% by weight, 95% by weight, and 99% by weight of the total weight of the composition of renewable isomeric paraffins.

In certain embodiments, the composition of renewable isomeric paraffins comprises at least 70% by weight, preferably at least 80% by weight, more preferably at least 90% by weight, and even more preferably at least 95% by weight paraffins based on the total weight of the composition of renewable isomeric paraffins, where from 60 to 95% by weight of said paraffins are isoparaffins, and where at least 80% by weight of said isoparaffins are in the range C14-C18 of the number of carbon atoms, and where the ratio of the amount in% by weight of isoparaffins with more than three branches to the amount in% by weight of the total isoparaffins is less than 0.15. The total amount of CO, CO: and C2H2 formed during the thermal cracking step is small, when the thermal cracking feed comprises or consists of such renewable isomeric paraffin compositions. In addition, these renewable isomeric paraffin compositions have good cold properties and good miscibility in fossil naphtha, and promote the formation of high-value cracking products, such as propene and ethene, in the cracking step. thermal.

As mentioned above, the renewable isomeric paraffin composition preferably contains a high weight % amount of paraffins. Accordingly, the renewable isomeric paraffin composition preferably comprises aromatic compounds (aromatic hydrocarbons) at 1.0 wt% or less, more preferably 0.5 wt% or less, even more preferably 0.2

wt% or less, and olefins (alkenes) at 2.0 wt% or less, preferably 1.0 wt% or less, preferably 0.5 wt% or less, and naphthenes (cycloalkanes) not more than 5.0% by weight, preferably 2.0% by weight or less.

A low wt% amount of aromatics, olefins and naphthenes in the composition of renewable isomeric paraffins promotes the formation of high value chemicals (HVC) in the thermal cracking step.

In this document, high value chemicals refer to ethene, propene, 1,3-butadiene, benzene, toluene and xylenes.

Benzene, toluene and xylenes can be called BTX.

In all cases, the composition of renewable isomeric paraffins preferably comprises a maximum of 50 ppm by weight of oxygen.

A low oxygen content allows thermal cracking to be carried out in a more controlled manner, which favors the formation of HVC.

The paraffins of the renewable isomeric paraffin composition are n-paraffins and i-paraffins.

Linear n-paraffins tend to crack into ethene molecules.

Therefore, it is preferred that the isomeric renewable paraffin composition comprises at least 5 wt%, such as 5 to 90 wt% n-paraffins of the total weight of paraffins in the isomeric renewable paraffin composition.

In certain embodiments, the composition of renewable isomeric paraffins comprises 5 to 40% by weight, preferably 8 to 35% by weight, more preferably 10 to 35% by weight, more preferably 20 to 35% by weight, and even better 30 to 35% by weight of n-paraffins of the total weight of the paraffins in the renewable isomeric composition.

In general, any composition of renewable isomeric paraffins as defined above can be used in any aspect or embodiment of the present invention.

Nevertheless, certain particularly preferred renewable isomeric paraffin compositions are mentioned below.

In certain particularly preferred embodiments, the composition of isomeric renewable paraffins comprises paraffins at at least 80% by weight of the total weight of the composition of isomeric renewable paraffins, in which 60 to 93% by weight of said paraffins are isoparaffins, and wherein of said isoparaffins, at least 90% by weight fall within the range of C14-C18 carbon atoms, and wherein the ratio of the amount in % by weight of isoparaffins with more than three branches on the percentage by total weight of the isoparaffins is less than 0.12. Furthermore, in certain particularly preferred embodiments, the composition of isomeric renewable paraffins comprises paraffins at 90% by weight of the total weight of the composition of isomeric renewable paraffins, in which, among said paraffins, 60 to 90% by weight, preferably 65 to 70% by weight, are isoparaffins, and wherein among said isoparaffins, at least 95% by weight are in the range C14-C18 of the number of carbon atoms, and wherein the ratio of the amount by weight of isoparaffins with more than three branches on the amount in % by total weight of isoparaffins is less than 0.10, preferably less than 0.5. These renewable isomeric paraffin compositions produce a particularly low total amount of CO, CO: and C2aHz while promoting the formation of HVC in the thermal cracking step when used as a thermal cracking feed or as a feed component thermal cracking in a mixture with fossil naphtha. In addition, these renewable isomeric paraffin compositions have favorable cold properties and mix well with (have good miscibility in) fossil naphtha.

Providing the thermal cracking feed may include providing the renewable isomeric paraffin composition and providing fossil naphtha, and combining the renewable isomeric paraffin composition with the fossil naphtha to form the thermal cracking feed. The composition of renewable isomeric paraffins is preferably obtained by subjecting a filler derived from renewable sources (renewable filler), the filler comprising fatty acids, fatty acid derivatives, mono-, di- or triglycerides, or a combination of these, to a hydrotreating to form n-paraffins, and subjecting at least a part of the n-paraffins formed in the hydrographic treatment to a treatment by isomerization to form i-paraffins.

Preferably, the renewable filler, i.e. the filler derived from renewable sources, comprises at least one vegetable oil, vegetable fat, animal oil or animal fat. These materials are preferred because they provide a renewable filler having a predictable composition which can be adjusted as needed by appropriate selection and/or blending of the natural oil(s) and/or fat(s). The renewable feed may include vegetable oil, wood oil, other vegetable oils, animal oil, animal fat, fish fat, fish oil, oil algae, microbial oil or a combination thereof. Optionally, the renewable feed may include recyclable waste and/or recyclable residue. Recyclable waste includes materials such as used cooking oils, free fatty acids, palm oil by-products or processing side streams, sludge, vegetable oil processing side streams or a combination of these. The overall sustainability of the renewable feed and, therefore, of the renewable isomeric paraffin composition and the cracked product formed can be increased by providing a renewable feed comprising recyclable waste or recyclable residue, or both, as such or combined with fresh foods of renewable oils and/or renewable fats, such as vegetable oil, vegetable fats, animal oil and/or animal fat.

Fresh food here refers to components that have not been recycled. The renewable feed may be subjected to an optional pretreatment before being subjected to hydrotreating and isomerization to obtain a composition of renewable isomeric paraffins.

This pretreatment may include purification and/or chemical modification of the renewable feed, such as saponification or transesterification.

If the renewable charge is a solid material (at ambient conditions), it is useful to chemically modify the material so as to obtain a liquid renewable charge, which is preferable.

Hydrotreating generally serves as a treatment for deoxygenation, denitrogenation and desulphurization of fatty acids, fatty acid derivatives and/or glycerides contained in the renewable feedstock.

Further, provided that the renewable isomeric paraffin composition includes subjecting the renewable feedstock to decarboxylation and decarbonylation reactions (i.e. removal of oxygen as COx) and/ or other catalytic processes to: remove oxygen from organic oxygen compounds as water, to remove sulfur from organic sulfur compounds as dihydrogen sulfide (H2S), remove nitrogen from organic compounds nitrogen in the form of ammonia (NHs) and to remove halogens from halogenated organic compounds, for example chlorine in the form of hydrochloric acid (HCl). These processes can be, for example, hydrodechlorination to remove chlorine and hydrodenitrogenation (HDN) to remove nitrogen.

Preferably, the hydrotreating is hydrodeoxygenation (HDO) or catalytic hydrodeoxygenation (catalytic HDO). The hydrotreatment is preferably carried out at a pressure chosen between 2 and 15 MPa, preferably between 3 and 10 MPa, and at a temperature chosen between 200 and 500°C, preferably between 280 and 400°C.

The hydrotreating can be carried out in the presence of a known hydrotreating catalyst containing metals from group VIII and/or VIB of the periodic system.

Preferably, the hydrotreating catalysts are supported Pd, Pt, Ni, NiW, NiMo or a CoMo catalyst, the support being alumina and/or silica.

In general, NiMo/Al203 and/or CoMo/Al20s catalysts are used.

The renewable isomeric paraffin composition of the present invention can be obtained by subjecting at least a part of the n-paraffins formed in the hydrotreating step to an isomerization treatment to form i-paraffins and to produce the paraffin composition renewable isomers.

The isomerization treatment is not particularly limited.

Nevertheless, catalytic isomerization treatments are preferred.

Generally, subjecting the n-paraffins formed during the hydrotreating step from the renewable feedstock to an isomerization treatment mainly forms methyl-substituted isoparaffins.

The severity of the isomerization conditions and the choice of catalyst determine the amount of methyl branches formed and their distance from each other in the carbon backbone.

The isomerization step may include other intermediate steps such as a purification step and a fractionation step.

The purification and/or fractionation steps allow better control of the properties of the composition of renewable isomeric paraffins in formation.

The isomerization treatment is preferably carried out at a temperature chosen between 200 and 500° C., preferably between 280 and 400° C., and at a pressure chosen between 2 and 15 MPa, preferably between 3 and 10 MPa.

The isomerization treatment can be carried out in the presence of known isomerization catalysts, for example catalysts containing a molecular sieve and/or a metal chosen from group VIII of the periodic table and a support.

Preferably, the isomerization catalyst is a catalyst containing SAPO-11 or SAPO-41 or ZSM-22 or ZSM-23 or ferrierite and Pt, Pd or Ni and Al2O3 or SiO2. Typical isomerization catalysts are, for example, Pt/SAPO-11/Al203, Pt/ZSM-22/Al203, Pt/ZSM-23/Al203 and/or Pt/SAPO-11/Si02. Catalyst deactivation can be reduced by the presence of molecular hydrogen in the isomerization process.

Therefore, the presence of added hydrogen in the isomerization treatment is preferable.

In some embodiments, the hydrotreating and isomerization catalysts are not in contact with the reaction feed (the renewable feed and/or the n-paraffins and/or the i-paraffins derived therefrom) at the same moment.

In some embodiments, the hydrotreating and isomerization are carried out in separate reactors or separately.

In certain embodiments, only a part of the n-paraffins formed during the hydrotreatment step is subjected to an isomerization treatment.

Part of the n-paraffins formed in the hydrotreating step can be separated, the separated n-paraffins then being subjected to the isomerization treatment to form i-paraffins.

After having been subjected to the isomerization treatment, the separated paraffins are optionally combined with the rest of the paraffins.

Alternatively, any n-paraffins formed in the hydrotreating step can be subjected to the isomerization treatment to form i-paraffins.

On the other hand, the isomerization treatment is a step which mainly serves to isomerize the paraffins of the composition of renewable isomer paraffins.

While most thermal or catalytic conversions (such as hydrotreating and PHDO) result in a low degree of isomerization (generally less than 5% by weight), the isomerization step which can be employed in the present invention is that which leads to a significant increase in the isoparaffin content of the composition of renewable isomeric paraffins.

Generally, the carbon number distribution does not change substantially during the isomerization treatment.

Consequently, the amount in % by weight of paraffins in the range C3-C14 of the number of carbon atoms does not increase significantly during the isomerization treatment.

This is favorable because isoparaffins with a carbon number lower than C14 increase the formation of CO, CO: and C2H2 in the thermal cracking step. Provided that the composition of renewable isomeric paraffins preferably does not include the gasification of a renewable feedstock. Paraffin compositions made by gas-liquid transformation (GTL) processes, such as processes comprising a step of the Fischer-Tropsch process, are characterized by a broad distribution of paraffinic hydrocarbons in the C9-C50 range of the number of carbon atoms, particularly C9-C24.

Water and light gases, such as carbon monoxide, carbon dioxide, hydrogen, methane, ethane and propane, can be separated from the hydrotreated and/or isomerized renewable feedstock by any conventional means, such as distillation, before supplying the composition of isomeric renewable paraffins as a thermal cracking charge or thermal cracking charge component. After or at the same time as the elimination of water and light gases, the hydrotreated and/or isomerized renewable feed can be fractionated into one or more fractions. The fractionation can be carried out by any conventional means, such as distillation. In addition, the hydrotreated and/or isomerized renewable feed can optionally be purified. Purification and/or fractionation allows better control of the properties of the isomeric paraffin composition being formed, and therefore of the properties of the cracked product from the thermal cracking step. However, a composition of renewable isomeric paraffins obtained by hydrotreating and isomerizing a renewable feedstock as described above can be fed directly into a thermal cracker or a thermal cracking process.

The content of isoparaffins and the types of isoparaffins (branching of isoparaffins) in the composition of revolving isomeric paraffins are mainly controlled by the isomerization treatment; for example, catalyst (or lack thereof), temperature, pressure, residence time and amount of hydrogen added in the isomerization process.

In some embodiments, providing the renewable isomeric paraffin composition includes analyzing the renewable isomeric paraffin composition obtained from the isomerization treatment and, based on the analysis results, selecting a isomeric renewable paraffin composition meeting the requirements described above and providing the selected isomeric renewable paraffin composition as a thermal cracking feedstock or as a thermal cracking feedstock constituent.

By choosing a composition of renewable isomeric paraffins that meets the criteria described above, the total amount of undesirable by-products, namely CO, CO: and C2Hz, formed during thermal cracking can be reduced.

Preferably, analysis of the composition of isomeric renewable paraffins comprises determining the % by weight of paraffins in the composition of isomeric renewable paraffins, determining the % by weight of isoparaffins in the composition of isomeric renewable paraffins, determining the ratio of the quantity in % by weight of the isoparaffins with more than three branches on the quantity in total % by weight of the isoparaffins in the composition of renewable isomeric paraffins and preferably the determination of the distribution of the number of carbon atoms of the isoparaffins in the composition of renewable isomeric paraffins.

The analysis of the composition of isomeric renewable paraffins can also comprise the determination of the % by weight of n-paraffins in the composition of isomeric renewable paraffins and/or the determination of the percentages by weight of monobranched, di- and trbranched isoparaffins and d isoparaffins with more than three branches, respectively.

The percentages by weight of paraffins, isoparaffins, n-paraffins, as well as monobranched isoparaffins, di- and tri-branched isoparaffins and isoparaffins with more than three branches can be determined by any suitable method, for example GC-analysis FID, like the analytical method described in the examples.

The thermal cracking charge of the present invention comprises, based on the total weight of the thermal cracking charge, 1 to 100% by weight of the renewable isomeric paraffin composition described above, and 0 to 99% by weight fossil naphtha, the sum of the amounts in % by weight of the composition of renewable isomeric paraffins and the fossil naphtha being at least 90 % by weight of the total thermal cracking charge. In other words, the renewable isomeric paraffin composition can be provided as a thermal cracking feedstock or as a component of the thermal cracking feedstock combined with fossil naphtha to form the thermal cracking feedstock. Preferably, the sum of the composition of renewable isomeric paraffins in percentage by weight and the amount of fossil naphtha in percentage by weight is at least 95% by weight, and more preferably at least 99% by weight of the weight total thermal cracking load. As used herein, fossil naphtha refers to a composition that is naturally occurring and comes from non-renewable sources. These non-renewable sources may also be referred to as "fossil sources" or "mineral sources". Non-renewable sources that fossil naphtha can come from include crude oil, petroleum oil or gas, shale gas or oil. , natural gas or coal, and the like, and combinations thereof, including any hydrocarbon-rich deposits that can be utilized from the ground or underground. These sources may also be referred to as "fossil oil". Fossil naphtha primarily includes hydrocarbons.In some embodiments, the fossil naphtha comprises hydrocarbons at at least 95% by weight, preferably at least 99% by weight, of the total weight of the fossil naphtha.In certain embodiments, the fossil naphtha comprises 20 to 85% by weight of paraffins, 0 to 30% by weight, preferably 0 to 5% by weight, of olefins (alkenes), 5 to 30% by weight of naphthenes (cycloalkanes) and 0 to 30% by weight of compounds flavored cs (aromatic hydrocarbons) relative to the total weight of fossil naphtha.

Fossil naphtha can be selected from various grades of fossil naphtha, such as heavy naphtha, light naphtha, or combinations thereof.

Preferably, the boiling point (from initial boiling point to final boiling point) of the fossil naphtha is in the temperature range of 25°C to 360°C.

In some embodiments, the boiling point of fossil naphtha is between 25°C and 220°C.

Additionally, in some embodiments, the boiling point of the fossil naphtha is between 30 and 90°C, preferably between 35 and 85°C.

Additionally, in some embodiments, the boiling point of the fossil naphtha is between 50°C and 200°C, preferably between 50°C and 187°C.

In some embodiments, the boiling point of fossil naphtha is between 180°C and 360°C.

Boiling point ranges are given as measured according to EN-ISO-3405 (2011). In some embodiments, the thermal cracking charge comprises, based on the total weight of the isomeric renewable paraffin composition, 50 to 100% by weight of the isomeric renewable paraffin composition, and 0 to 50% by weight of naphtha fossil.

In certain preferred embodiments, the thermal cracking charge comprises, based on the total weight of the thermal cracking charge, 50 to 85% by weight of the renewable isomeric paraffin composition and 15 to 50% by weight of fossil naphtha , preferably 60 to 85% by weight of the composition of renewable isomeric paraffins and 15-40% by weight of fossil naphtha, more preferably 70 to 85% by weight of the composition of renewable isomeric paraffins and 15-30% by weight of fossil naphtha.

A thermal cracking charge comprising at least 50% by weight of the isomeric renewable paraffin composition, or comprising mainly the isomeric renewable paraffin composition, is preferred. The composition of renewable isomeric paraffins promotes the formation of HVC in the thermal cracking step compared to fossil naphtha and increases the durability of the thermal cracking feed, and therefore the durability of the cracked product formed. In some embodiments, the thermal cracking feed comprises the composition of renewable isomeric paraffins and fossil naphtha in a weight ratio of 5:1 (composition of renewable isomeric paraffins to fossil naphtha).

The thermal cracking of the present invention is preferably steam cracking. Steam cracking plants are widely used in the petrochemical industry and in particular as a source of raw materials for the polymer industry. The process conditions for steam cracking are well known, therefore the practice of the present invention requires little modification of established processes. The thermal cracking of the thermal cracking charge described above is preferably carried out in a conventional naphtha (steam) cracker, i.e. a cracker commonly used for the thermal cracking of fossil naphtha. The thermal cracking is preferably carried out without a catalyst. However, additives, in particular sulfur additives, can be used in the thermal cracking step. The process of the present invention may include providing a thermal cracking feed comprising sulfur to reduce coke formation and to further reduce CO and CO2 formation in the thermal cracking step. The formation of C2zH2 in the thermal cracking step is not significantly influenced by the sulfur content of the thermal cracking charge. Without being bound by any theory, it is believed that the sulfur passives the active sites on the surface of the cracker coil, in particular the Ni sites of the cracker coil material, by forming nickel sulphides. Nickel sulphides do not catalyze the gasification of coke, unlike the metallic oxides of Ni and

Neither.

To further reduce the formation of CO and CO2 in the thermal cracking step, the thermal cracking charge may contain sulfur.

The compositions of renewable isomeric paraffins obtained by hydrotreating and isomerizing renewable feedstocks, in particular vegetable and/or animal oils/fats, are chemical mixtures of mainly paraffinic hydrocarbons comprising a very small quantity of sulphur.

Without additivation of sulfur, the composition of renewable isomeric paraffins can contain less than 5 ppm of sulfur by weight.

Sulfur can be added to the thermal cracking charge by adding a sulfur-containing compound (sulphur-based additive) to the thermal cracking charge, or by providing a thermal cracking charge comprising the composition of renewable isomeric paraffins and an amount sufficient amount of fossil naphtha generally comprising sulphur, or both.

Accordingly, in some embodiments, the thermal cracking feed comprises sulfur at 20 to 300 ppm by weight, preferably 20 to 250 ppm by weight, preferably 20 to 100 ppm by weight, and even more. from 20 to 65 ppm by weight.

Since the renewable isomeric paraffin composition of the present invention already reduces the total amount of undesirable by-products (CO, COz and CzH2) formed during thermal cracking, the thermal cracking feed need not contain large amounts of sulfur.

A low sulfur concentration of the thermal cracker feed has the advantage that the cracked product, especially its heavier hydrocarbon fractions, also has a low sulfur content.

Generally, the heavier hydrocarbon fractions of the cracked product (C4 and above) are not subjected to extensive purification after being separated from the cracked product, and therefore the sulfur from the thermal cracking step remains essentially in these fractions .

The pyrolysis gasoline (PyGas) fraction, which usually comprises mainly C4-C11 hydrocarbons, especially C5-C9 hydrocarbons from which benzene has been removed, is usually diverted to a fuel reserve, i.e. i.e. used as a combustible component.

Low or ultra-low sulfur fuels and fuel components are preferred because low sulfur fuels or sulfur-free fuels produce fewer harmful emissions during combustion than low sulfur fuels or fuel components. higher sulfur content.

A thermal cracking charge comprising 50 to 65 wppm sulfur is particularly preferred because a sulfur content of 50 to 65 wppm further reduces the formation of CO and CO2 in the thermal cracking step and forms a PyGas fraction with low sulfur content (without post-fraction purification steps). Dimethyl disulfide (DMDS), hydrogen sulfide (H2S) and carbon disulfide (CS:2) are examples of suitable sulfur-based additives.

DMDS is a particularly popular sulfur-based additive because it reduces coking.

In certain embodiments, provided that the thermal cracking charge comprises mixing a sulfur-based additive, preferably DMDS, with the thermal cracking charge to form a thermal cracking charge comprising 20 to 300 ppm in weight of sulphur, preferably 20 to 250 ppm by weight, more preferably 20 to 100 ppm by weight, even more preferably 20 to 65 ppm by weight.

In certain preferred embodiments, provided that the thermal cracking charge comprises mixing a sulfur-based additive, preferably DMDS, with the thermal cracking charge to form a thermal cracking charge comprising 50 to 65 ppm by weight of sulphur.

The sulfur-based additive may be mixed with the thermal cracking charge before feeding the thermal cracking charge to the thermal cracking step.

Optionally, a sulfur-based additive can be added to the thermal cracking step by injection into a steam thermal cracking furnace comprising a sulfur-based additive.

Accordingly, in some embodiments, the process includes injecting into a thermal cracking furnace steam comprising a sulfur-based additive, preferably DMDS, such that the thermal cracking charge in the thermal cracking furnace comprises sulfur in an amount of 20 to 300 ppm by weight, preferably 20 to 250 ppm by weight, more preferably 20 to 100 ppm by weight, even more preferably 20 to 65 ppm by weight.

In certain preferred embodiments, the process comprises injecting into a thermal cracking furnace steam comprising a sulfur-based additive, preferably DMDS, such that the thermal cracking charge in the furnace comprises sulfur at from 50 to 65 ppm by weight.

In some embodiments, providing the thermal cracking charge comprises combining fossil naphtha with the renewable isomeric paraffin composition to form a thermal cracking charge comprising 20 to 300 ppm by weight sulfur, preferably 20 to 250 ppm by weight, more preferably 20 to 100 ppm by weight, even more preferably 20 to 65 ppm by weight.

In certain preferred embodiments, provided that the thermal cracking charge comprises combining fossil naphtha with the renewable isomeric paraffin composition to form a thermal cracking charge comprising 50 to 65 ppm by weight sulfur.

The sulfur concentration of fossil naphtha can vary depending on the source of the fossil naphtha and the refining steps to which it has been subjected.

Providing a thermal cracking charge comprising a predetermined amount of sulfur may include selecting fossil naphtha with an appropriate sulfur content, adjusting the weight percentage of fossil naphtha in the thermal cracking charge, or both.

A thermal cracking charge comprising a predetermined amount of sulfur can therefore be supplied without the addition of a sulfur-based additive.

However, a sulfur-based additive may optionally be added to a thermal cracking charge comprising fossil naphtha and the renewable isomeric paraffin composition.

By providing as the thermal cracking charge the thermal cracking charge of the present invention, a favorable low amount of impurities (CO, COz, C:2H2) can be obtained by carrying out the thermal cracking step at an exit temperature of coil (TOC) selected from a wide range of temperatures. TOC is generally the highest temperature for the thermal cracking load in the thermal cracker. The thermal cracking step is preferably carried out at a TOC chosen between 780 and 890°C, preferably between 800 and 860°C. The total amount of undesirable by-products (CO, CO2 and C:2H2) formed during the thermal cracking step is particularly low when the TOC is chosen between 800 and 840°C. The TOC can, for example, be selected from about 805°C, 810°C, 815°C, 820°C, 825°C, 830°C, and 835°C. A particularly low total amount of undesirable by-products (CO, CO2 and C2H2) are formed when thermal cracking is carried out at a TOC of around 800°C. Thermal cracking feeds comprising both the renewable isomeric paraffin composition and the fossil naphtha form particularly low amounts of CO, CO 2 and C 2 H 2 when the TOC is selected in the range of 800°C to 820°C.

In some embodiments, where the thermal cracking is steam cracking, the steam cracking is performed at a flow rate ratio between water and thermal cracking feed (H2O flow [kg/h] / feed flow thermal cracking [kg/h]) from 0.05 to 1.20, preferably 0.10 to 1.00, even more preferably 0.20 to 0.80, even more preferably 0.25-0.70 and even more preferably 0.25-0.60 and even more preferably 0.30-0.50. In certain preferred embodiments, where the thermal cracking is steam cracking, the steam cracking is carried out at a flow rate ratio between water and the thermal cracking feed (H2O flow [kg/h] / flow rate thermal cracking load [kg/h]) from 0.30 to 0.50 and at a TOC chosen between 800°C and 840°C.

Under these conditions, steam cracking results in a low total amount of CO, CO: and C2H2. The outlet pressure of the coil in the thermal cracking step can be chosen between 0.09 and 0.3 MPa, preferably at least 0.1 MPa, more preferably at least 0.11 MPa or 0.12 MPa, preferably at most 0.25 MPa, preferably at most 0.22 MPa or 0.20 MPa.

The thermal cracking process may include recycling unconverted reactants to the thermal cracking furnace.

As an option, some less valuable parts of the cracked product, such as propane and ethane, can be recycled in the thermal cracking furnace to be converted into more valuable products, such as ethene and propene.

Recycling unconverted reactants, less valuable parts of the cracked product, or both, increases the overall economics and overall yield of the thermal cracking process and/or overall HVC yield.

Thermal cracking can be carried out in multiple thermal cracking furnaces.

The thermal cracking charge of the present invention comprising or consisting of the renewable isomeric paraffin composition may be introduced into one or more of the multiple thermal cracking furnaces.

For example, the availability of the renewable isomeric paraffin composition may determine how many multiple thermal cracking furnaces can be fed with the thermal cracking feedstock of the present invention.

Effluents or cracking products from multiple steam crackers can be combined to form one or more effluent streams that may be transported or conveyed to other processing steps, such as purification and/or polymerization.

Optionally, the thermal cracking can be performed in a single thermal cracking furnace fed by the thermal cracking feed of the present invention, and the effluent or cracking product from the single thermal cracking furnace can optionally be conveyed or transported to further processing steps, such as purification and/or polymerization.

The steam cracking process may include quenching and cooling the cracked product. Typically, at least some of the CO, CO2, C2H2 or a combination thereof is removed from the cracked product during quenching and cooling. In some embodiments, the process comprises fractionating the cracked product comprising a mixture of hydrocarbons. Fractionation may include separation of the cracked product from a fuel oil fraction, a PyGas fraction, a hydrogen fraction, a methane fraction, a fuel gas fraction, a C2 fraction (ethylene fraction), a C3 fraction (propylene fraction), and/or a C4 fraction. The C2 fraction (ethylene fraction) and the C3 fraction (propylene fraction) are particularly suitable for the production of polymers. Thus, in some embodiments, the process comprises separating from the cracked product an ethylene fraction, a propylene fraction, or both, and subjecting the ethylene fraction, the propylene fraction or both to a polymerization treatment.

The present invention makes it possible to obtain a cracked product having a low total amount of CO, CO2 and C:H2 by thermal cracking the thermal cracking charge of the present invention.

In some embodiments, the cracked product includes one or more of hydrogen, methane, ethane, ethene, propane, propene, propadiene, butane, butenes, such as butene, isobutene and butadiene, C5+ hydrocarbons such as aromatic compounds, benzene, toluene, xylenes, C5-C18 paraffins, C5-C18 olefins. Optionally, at least part of the hydrocarbons contained in the cracking product can be transformed into one or more derivatives, such as a derivative of methane or derivatives of methane, a derivative of ethene or derivatives of ethene, a propene derivative or propene derivatives, a benzene derivative or benzene derivatives, a toluene derivative or toluene derivatives, and/or a xylene derivative or xylene derivatives.

Methane derivatives include, for example, ammonia, methanol, phosgene, hydrogen, oxochemicals and their derivatives, such as methanol derivatives. Methyl methacrylate, polymethyl methacrylate, formaldehyde, phenolic resins, polyurethanes, methyl-tert-butyl ether and their derivatives are examples of methanol derivatives.

Ethylene derivatives include, for example, ethylene oxide, ethylene dichloride, acetaldehyde, ethylbenzene, alpha-olefins and polyethylene, and their derivatives, such as derivatives of ethylene oxide, ethylbenzene derivatives and acetaldehyde. Ethylene oxide derivatives include, for example, ethylene glycols, ethylene glycol ethers, ethylene glycol ether acetates, polyesters, ethanolamines, ethyl carbonates and their derivatives. Ethylbenzene derivatives include, for example, styrene, acrylonitrile-butadiene-styrene, styrene-acrylonitrile resin, polystyrene, unsaturated polyesters, styrene-butadiene rubber and their derivatives. Acetaldehyde derivatives include, for example, acetic acid, vinyl acetate monomer, polyvinyl acetate polymers and their derivatives. Ethyl alcohol derivatives include, for example, ethyl amines, ethyl acetate, ethyl acrylate, acrylic elastomers, synthetic rubber and their derivatives. In addition, ethene derivatives include polymers, such as polyvinyl chloride, polyvinyl alcohol, polyester such as polyethylene terephthalate, polyvinyl chloride, polystyrene and their derivatives.

Propene derivatives include, for example, isopropanol, acrylonitrile, polypropylene, propylene oxide, acrylic acid, allyl chloride, oxoalcohols, cumens, acetone, acrolein , hydroquinone, isopropylphenols, 4-hethylpentene-1, alkylates, butyraldehydes and ethylene-propylene elastomers and their derivatives. Propylene oxide derivatives include, for example, propylene carbonates, allyl alcohols, isopropanolamines, propylene glycols, glycol ethers, polyether polyols, polyoxypropyleneamines, 1,4-butanediol and their derivatives. Allyl chloride derivatives include, for example, epichlorohydrin and epoxy resins. Isopropanol derivatives include, for example, isopropyl acetate, isophorone, methyl methacrylate, polymethyl methacrylate, and their derivatives. Butyraldehyde derivatives include, for example, acrylic acid, acrylic acid esters, isobutanol, isobutylacetate, n-butanol, n-butylacetate, ethylnexanol and their derivatives. Acrylic acid derivatives include, for example, acrylic esters, polyacrylates and water-absorbent polymers, such as superabsorbents, and their derivatives. Butylene derivatives include, for example, alkylates, methyl-tert-butyl ether, ethyl-tert-butyl ether, polyethylene copolymer, polybutenes, valeraldehyde, 1,2-butylene oxide, propylene, octenes, sec-butyl alcohol, butylene rubber, methyl methacrylate, isobutylenes, polyisobutylenes, substituted phenols such as p-tert-butylphenol, di-tert-butyl-p-cresol and 2,6-di-tert-butylphenol, polyols and their derivatives. Other butadiene derivatives can be styrene butylene rubber, polybutadiene, nitrile, polychloroprene, adiponitrile, acrylonitrile butadiene styrene, styrene-butadiene copolymer latexes, styrene block copolymers, and styrene-butadiene rubber.

Benzene derivatives include, for example, ethylbenzene, styrene, cumene, phenol, cyclohexane, nitrobenzene,

alkylbenzene, maleic anhydride, chlorobenzene, benzene sulfonic acid, biphenyl, hydroquinone, resorcinol, polystyrene, styrene-acrylonitrile resin, styrene-butadiene rubber, acrylonitrile-butadiene-styrene resin , styrene-block copolymer, bisphenol-A, polycarbonate, methyl-diphenyl diisocyanate, and their derivatives. Cyclohexane derivatives include, for example, adipic acid, caprolactam and their derivatives. Nitrobenzene derivatives include, for example, aniline, methylene diphenyl diisocyanate, polyisocyanates and polyurethanes. Alkylbenzene derivatives include, for example, linear alkylbenzene. Chlorobenzene derivatives include, for example, polysulfone, polyphenylene sulfide and nitrobenzene. Phenol derivatives include, for example, bisphenol A, aldehyde resins in the form of phenol, cyclohexanone-cyclohexenol mixture (KA oil), caprolactam, polyamides, alkylphenols, such as p-nonoylphenol and p-dedocylphenol , ortho-xylenols, aryl phosphates, o-cresols, cyclohexanol.

Toluene derivatives include, for example, benzene, xylenes, toluene diisocyanate, benzoic acid and their derivatives.

Xylene derivatives include, for example, aromatic diacids and anhydrates, such as terephthalic acid, isophthalic acid, phthalic anhydride and phthalic acid, and their derivatives. Terephthalic acid derivatives include, for example, terephthalic acid esters, such as dimethyl terephthalate, and polyesters, such as polyethylene terephthalate, polytrimethylene terephthalate, polybutylene terephthalate and polyester polyols. Phthalic acid derivatives include, for example, unsaturated polyesters and plasticizers for PVC. Isophthalic acid derivatives include, for example, unsaturated polyesters, polyethylene terephthalate copolymers and polyester polyols.

The cracked product hydrocarbons obtained by the process of the present invention are particularly suitable as raw materials for conventional petrochemicals, and in particular for the polymer industry.

More specifically, the mixture of hydrocarbons included in the cracked product obtained by the process of the present invention shows a product distribution similar, even favorable (including a higher % by weight of HVC), to the product distribution of the hydrocarbons obtained by thermal cracking (steam cracking) compared to conventional fossil raw materials, such as naphtha.

It is thus possible to produce, for example, polymers partly derived from renewable materials by providing as thermal cracking charge the thermal cracking charge of the present invention.

Optionally, polymers derived exclusively from renewable materials can be produced by providing as the thermal cracking charge a thermal cracking charge of the present invention consisting of the composition of renewable isomeric paraffins.

In some embodiments, the process includes subjecting at least a portion of the cracked product to a purification treatment to remove at least one of the compounds CO, CO: or C2Ha.

An advantage of the process of the present invention is a low total amount of CO, COz and C2H2 in the cracked product formed during the thermal cracking step and, therefore, a reduction in the CO, CO2 removal load. , C:H2, or a combination thereof, of the cracked product.

This is particularly advantageous in embodiments where at least a portion of the cracked product is subjected to a polymerization treatment.

As mentioned previously, CO, CO2 and C2H2 are polymerization catalyst poisons and are therefore undesirable in a polymerization process.

The task of removing CO, CO2, C2H2, or a combination thereof, from a portion of the cracked product to be subjected to a polymerization treatment can be significantly reduced, and potentially even unnecessary. In practice, however, part of the cracked product to be subjected to a polymerization treatment is usually first subjected to a purification treatment, for example as a precaution or to avoid any deviation from standard procedures. In any case, a lower amount of CO, CO: and/or C2H2 impurities in the cracking product increases the life of the active material, such as absorbent, adsorbent, reagent, molecular sieve and / or a purification catalyst, which can be used in the purification treatment to eliminate at least one compound among CO, CO2 or C2H2, and decreases the frequency of regeneration of the active material.

The purification treatment to which at least a part of the cracking product can be subjected can be any suitable purification treatment to eliminate at least one compound among CO, CO: or C2H2. Examples of such purification treatments are described in EP2679656A1, WO2016023973, WO2003048087 and US2010331502A1, all of which are incorporated as a whole herein by reference.

In certain embodiments, the purification treatment comprises contacting at least a portion of the cracked product with an active material, such as an absorbent, an adsorbent, a purification catalyst, a reagent, a molecular sieve or a combination thereof, to remove at least one of CO, CO2, or C:H2. Optionally, the purification treatment may include contacting at least a portion of the cracked product with the active material in the presence of molecular oxygen, molecular hydrogen, or both. In some embodiments, the purification treatment includes passing at least a portion of the cracked product through at least one purification train comprising active material, or at least one bed of active material. Contact can be made in a single container. Optionally, the contacting can be carried out in several vessels, preferably connected in series, i.e. allowing the part of the cracked product to be purified to be passed from one vessel to another for purification. later. The active material can comprise, for example, copper oxide or a catalyst based on copper oxide, oxides of Pt, Pd, Ag, V, Cr, Mn, Fe, Co, or Ni optionally supported on alumina, Au/Ce02 optionally supported on alumina, zeolites, in particular type A and/or type X zeolites, alumina-based absorbents or catalysts such as a Selexsorbru COS or Selexord™ CD, a molecular sieve comprising alumina, aluminosilicate aluminophosphates or mixtures thereof, or any combination of these substances. The active material may comprise an adsorbent or adsorbents as described in WO03/048087A1 on pages 11,1112-p. 12, ll. 3; p. 12, He. 18 - p. 15, He. 29, and/or p. 17, He. 21, p. 21, Il. 2 and/or a molecular sieve or molecular sieves described in WO03/048087A1 at pages 21, II. 3 - p. 22 He. 26. The active ingredient may comprise one or more purification catalysts as described in paragraphs

[0105] to [0116] of document US2010/0331502A1, or one or more molecular sieves as described in paragraphs [0117] to [0119] of document US2010/0331502A1. The active ingredient may comprise one or more purification catalysts described in paragraph [0061], [0062],

[0063], and/or [0064] of document WO2016/023973A1. The purification treatment may be a purification treatment as described in document EP2679656A1, paragraphs [0043] to

[0082]. The purification treatment can be a purification treatment as described in paragraphs [0092] to [0119], and/or in paragraph [0126], and/or in example 2 of document US2010/0331502A1. The purification treatment can be a purification treatment as described in paragraphs [0056] to [0067] of document WO2016/023973A1. The purification treatment can be a purification treatment as described in WO03/048087A1, p. 11, He. 12 - p. 15, He. 29, and/or p. 16, He. 1 - p. 21, Il. 2, and/or p. 23, Il. 14 - p. 24, Il. 13, and/or Example 1 and/or Example

2. Generally impurities deactivate or foul the active ingredient during the purification process. Thus, the active material can be regenerated to at least partially regain its purification activity. Any regeneration method making it possible to reactivate the active material can be used. For example, the active material can be regenerated as described in WO2016/023973A1, paragraphs p. 12, He. 3 to 10, or as described in EP2679656A1, paragraphs [0108] to [0118], or as described in WO03/048087A1, p. 24, Il. 14 - p. 25 He. 32. For example, a CuO catalyst can be regenerated by contacting the CuO catalyst with Hz. A CuO2 catalyst can be regenerated by contacting the CuO2 catalyst with molecular oxygen. A zeolite molecular sieve can be regenerated by applying heat and contacting the zeolite molecular sieve with an inert gas stream, such as a nitrogen stream.

In some embodiments, the purification treatment includes at least one of the following steps: i) contacting at least a portion of the cracked product with a CuO catalyst to remove oxygen, ii) contacting at least a portion of the cracked product with H2 to remove C2H2 by hydrogenation, iii) contacting at least a portion of the cracked product with a CuO catalyst: to remove CO by oxidation, or iv) contacting at least a portion of the cracked product with a zeolitic molecular sieve to remove COa.

Optionally, the purification treatment can comprise the elimination of secondary impurities, such as at least one of the compounds among COS, H2S or CSz, by bringing into contact at least a part of the cracking product with a catalyst of activated alumina, such as SelexorbTM.

In some embodiments, the method includes subjecting at least a portion of the cracked product to a polymerization treatment to form polymers.

The part of the cracked product subjected to the polymerization treatment can be obtained directly by the thermal cracking process or by the purification treatment described in the previous sections.

Optionally, the part of the cracked product subjected to the polymerization treatment may have been partly subjected to the purification treatment described in the previous sections and partly obtained directly from the thermal cracking process.

As mentioned before, due to the low amount of CO, COz and C2H2 in the cracked product formed during the thermal cracking step, subject the cracked product or part of it to a purification treatment before polymerization may be redundant.

In certain preferred versions, the part of the cracking product subjected to the polymerization treatment is an ethylene fraction, a propylene fraction or a combination thereof.

Accordingly, in some embodiments, the process includes subjecting an ethylene fraction of the cracked product to a polymerization treatment to form polyethylene, and optionally subjecting a propylene fraction of the cracked product to a polymerization treatment to form polypropylene.

The polymerization treatment may include solution polymerization, gas phase fluidized bed polymerization, suspension polymerization, such as bulk polymerization, high pressure polymerization, or a combination thereof.

The polymerization treatment can be carried out in one or more polymerization reactors.

Each of the one or more polymerization reactors may comprise several polymerization zones.

The composition of the charge fed into the polymerization zones may vary from one zone to another.

For example, different portions of the cracked product may be fed to different zones and a comonomer may optionally be introduced into one or more of the polymerization zones.

The comonomer feeding the polymerization zones can be a different comonomer for different polymerization zones.

The polymerization reactor may, for example, be a continuous stirred tank reactor, a fluidized bed reactor, such as a gas phase fluidized bed reactor, or a stirred gas phase fluidized bed reactor in horizontal or vertical configuration .

Preferably, the polymerization treatment is catalytic polymerization.

In some embodiments, the polymerization treatment includes contacting at least a portion of the cracked product with a polymerization catalyst, optionally in the presence of molecular hydrogen to form polymers.

The contacting is preferably carried out in one or more polymerization reactors.

In embodiments, where the polymerization treatment is a catalytic polymerization treatment, the molecular weight of the polymers formed can be regulated, for example, by the presence of hydrogen in the polymerization treatment or by the control of the temperature of reaction, depending on the polymerization catalyst(s) used.

In the embodiments, where the polymerization treatment is a catalytic polymerization treatment, the polydispersity is mainly controlled by the catalyst used.

The polymerization treatment can be a polymerization treatment forming polymers having monomodal, bimodal or multimodal molecular weight distributions.

Bimodality or multimodality can be obtained using a bifunctional catalytic system in a reaction medium (i.e. a reactor or a polymerization zone), or with a typical catalyst (i.e. non-bifunctional ) but with variable reaction media (i.e. a combination of several polymerization zones or several polymerization reactors with different feeds). Other properties of the polymers formed in the polymerization process, such as polarity, unsaturation content, and/or polydispersity, can be controlled by controlling reaction temperature, pressure, and residence time, or by injecting a predetermined type and quantity of co- and/or termonomers in the polymerization process at a predetermined location, for example in one or more of the polymerization zones optionally included in the polymerization reactor(s). Optionally, the density, modulus of elasticity and other properties of the polymers formed in the polymerization treatment can be controlled by introducing into the polymerization treatment a comonomer or combinations of multiple monomers, for example at least one of the ethylene (in polypropylene production), propylene (in polyethylene production), butene-1, 1-hexene (also (1,5-hexadiene), 1-octane (also 1,7-octadiene) and decene-1 (also 1,9-octadiene) or higher alpha olefins or alpha omega dienes.

In some embodiments, the polymerization treatment is a slurry polymerization treatment comprising dissolving in a diluent, such as propane, propene, or hexane, at least a portion of the cracked product with molecular hydrogen, and optionally a comonomer, to form a solution and contacting the solution with a catalyst to form the polymers.

In certain embodiments, the polymerization treatment is a high pressure polymerization preferably carried out in an autoclave reactor or a tubular reactor. Generally, high pressure polymerization does not use catalysts. Both the autoclave reactor and the tubular reactor can comprise several polymerization zones in which at least a part of the cracking product can optionally be fed with a comonomer. The composition of filler supplied to the polymerization zones may vary from zone to zone, as indicated above. High pressure polymerization can be initiated with various initiators such as molecular oxygen, organic t-amyl peroxide, or t-butyl peroxy-esters, or mixtures thereof. The molecular weight of polymers formed during high pressure polymerization can optionally be controlled using chain transfer agents, such as methyl ethyl ketone (MEK), propionaldehyde, alpha-olefins, di-olefins, or a combination of these. In certain preferred embodiments, the cracked product fraction subjected to high pressure polymerization is the ethylene fraction. Examples of polymers that can be formed during the high pressure polymerization of the ethylene moiety are low density polyethylene (LDPE), LDPE copolymers or LDPE terpolymers with vinyl acetate and/or other esters, such as methyl, ethyl or butyl acrylates, glycidyl methacrylate, and/or acid groups, such as acrylic or methacrylic acid, and/or silanes, such as vinyltrimethoxysilane and/or acid anhydrides , such as maleic anhydride. The polymerization treatment may be a polymerization treatment as described in EP2679656A1, paragraphs [0090] to

[0097]. The polymerization treatment can be a polymerization treatment as described in paragraphs [0050] to [0066] and/or

[0123] to [0125], and/or in Example 3 of document US2010/0331502A1. The polymerization treatment may be a polymerization treatment as described in paragraphs [0006] to [0020] and/or [0024] to [0043] of document WO2016/023973. The method may comprise a combination of a purification treatment and a polymerization treatment as described in paragraphs [0092] to [0119] of document US2010/0331502A1.

Preferably, the part of the cracked product subjected to the polymerization treatment is an ethylene fraction of the cracked product and polyethylene (PE), or its co- or terpolymers, is thus formed in the polymerization treatment.

The cracked product ethylene monomers can be homopolymerized or copolymerized with one or more comonomers, such as 1-propylene, 1-butene, 1-pentene, 1-hexene, 1-octene and/or conjugated and unconjugated diolefins, such as butadiene, 1,3-pentadiene, 2,3-dimethylbutadiene, 1,4-pentadiene, 1,5-hexadiene and or vinylcyclohexene.

Preferably, ethylene is copolymerized with 1-butene, 1-octene or 1-hexene.

Examples of polymerization processes to form PE, or co- or terpolymers thereof, include single-modal processes, and/or multi-modal processes, including hybrid processes.

Linear polyethylene of various densities range from ultra-low density polyethylene (ULDPE), very low density polyethylene (VLDPE), linear low density polyethylene (LLDPE), medium density polyethylene (MDPE) to homo/copolymers of high density polyethylene (HDPE), block or random co/terpolymers to multimodality can be formed in the polymerization treatment of the ethylene moiety by, for example, suspension or bulk polymerization (The. a process diluent in suspension and a monomer are identical), solution phase polymerization, gas phase polymerization and/or combinations of several reactors of identical or hybrid technologies operating in parallel or in series (known as cascade) producing similar polymers (c that is to say monomodal) or different (that is to say bi-modal, trimodal or multimodal) in different ratios, or being distributed over each reactor.

The part of the cracked product subjected to the polymerization treatment may preferably be the propylene fraction of the cracked product and the polypropylene (PP), or its co- or terpolymers, is thus formed in the polymerization treatment.

Polypropylenes of different density ranges and product classes, such as homopolymers, high crystallinity homopolymers, high crystallinity homopolymers, random copolymers, impact copolymers, block copolymers, heterophasic copolymers or combinations thereof, can be formed in the polymerization treatment of the propylene moiety.

An example of a polymerization catalyst for the catalytic polymerization, in particular of the ethylene fraction and/or the propylene fraction, is that of Ziegler-type catalysts, which use aluminum alkyl compounds, such as trimethylaluminium, triethylaluminum, tri-isobutylaluminum, methylaluminoxane (MAO) or tri-n-hexylaluminum as a cocatalyst to activate the titanium and vanadium sites of the catalyst, such as titanium tetrachloride. The aluminum alkyl compounds can also be used as agents for trapping polymerization poisons in the reaction media.

The polymerization catalyst for the catalytic polymerization can be supported if desired or required by the process. The support material can be magnesium dichloride or a silica support onto which active sites and optionally internal donors, such as benzoate, phthalate, diether or succinate, can be impregnated. Also, external donors, such as ethyl p-ethoxybenzoate (PEEB), dicyclopentyldimethoxysilane (DCPMS), diisopropyldimethoxysilane (DIPS), diisobutyldimethoxysilane, cyclohexyldimethoxymethylsilane (CHMMS), dicyclopentyldimethoxysilane (DPDMS) or alkoxysilanes, such as Me(EtO)3Si, Ph(EtO)3Si,Ph2(MeO)2Si, Ph2(EtO)2Si, Ph2(EtO)2Si, Ph(EtO)3Si can be added to the polymerization process.

In some embodiments, the polymerization catalyst is a stereo modifier, such as cyclohexylmethyldimethoxysilane, diisobutyldimethoxysilane, diisopropyldimethoxysilane,

Visobutylisopropyldimethoxysilane, n-propyltrimethoxysilane, Visobutylmethyldimethoxysilane, tetraethoxysilane, tetraethoxysilane, isobutyltriethoxysilane, n-propyltrimethoxysilane, Visobutyltrimethoxysilane and/or cyclohethyldimethoxysilane. Another example of a polymerization catalyst for the catalytic polymerization, in particular of the ethylene fraction and/or the propylene fraction, are the so-called single-site catalyst systems of which there are several types, such as Kaminsky type, combined type, constrained geometry type and late transition metal type.

The polymerization catalyst may contain a metallocene complex of zirconium, titanium or hafnium which usually contains two cyclopentadienyl rings or one-lobed equivalents of cyclopentadienyl and either a perfluorinated aromatic boron compound, or an organoaluminum compound, or methylaluminoxane whose rings contain various alkyl, linear and cyclic substituents. These cycles can be linked together by bridging groups. Alternatively, the polymerization catalyst may contain monocyclopentadienyl derivatives of titanium or zirconium, one of the carbon atoms of the cyclopentadienyl ring being additionally linked to the metal atom by a bridge.

These complexes which may be contained in the polymerization catalyst are generally converted into polymerization catalysts by reaction of said complexes with methylaluminoxane or by formation of ionic complexes with non-coordinating anions. Other complexes, such as ketimide group 4 cyclopentadienyl complexes, cyclopentadienyl group 4 siloxyl complexes and/or non-cyclopentadienyl group 4 phosphinimide complexes, may optionally be used to form polymerization catalysts.

Another type of polymerization catalysts for catalytic polymerization are Phillips type catalysts which may comprise hexavalent chromium supported on a large pore, high surface area oxide support, such as silica, alumina, titanium, aluminophosphates, or combinations where a mixture of chromium oxide and silicon (CrO3/SIO2) can be used to create active sites. The polymerization catalyst may be a polymerization catalyst as described in EP2679656A1, paragraphs [0098] to

[0107]. The polymerization catalyst may be a polymerization catalyst as described in US2010/0331502A1, paragraphs

[0067] to [0091], and/or Example 1. The polymerization catalyst may be a polymerization catalyst as described in WO2016/023973A1, paragraphs [0045] to [0055].

The properties of polymers formed in a catalytic polymerization process, such as molecular weight, molecular weight distribution, long chain branching content, density, viscosity, crystallinity, amorphous content, thinning behavior in shear, other rheological parameters, composition distribution indicators such as comonomer distribution breadth index (CDBI), comonomer distribution constant (CDC), thermal stability, melting temperature, temperature crystallization rate, melt index (MFR) and other factors can be influenced by the choice of catalyst type or types of catalysts (there are hybrid versions and it is possible to feed two or more catalysts different in one or more reactors), the type of comonomer, the comonomer content, the additional monomer(s) and their type and quantity(s).

After the polymerization process, the polymers formed can be modified to form martial polymers. The polymers formed can be modified by one or more extrusion or compounding steps during which additional ingredients are optionally added. These additional ingredients are, for example, stabilizing additives, impact modifiers such as plastomers or elastomers, other components of mixtures in general, fillers such as talc, glass fibres, carbon, nanoclays or other nanomaterials, carbon black, nucleating agents (which may also be added in situ during polymerization processing or polymerization catalyst preparation), UV stabilizers, pigments, crosslinking agents or viscera such as organic peroxides, acid scavengers such as calcium stearate, polymer treating agents, e.g. fluoropolymers Additional comonomers or functional groups, such as silanes and/or maleic anhydride, may optionally be added to the polymers formed after the reactive extrusion polymerization treatment. The polymers formed can, after the polymerization treatment, be subjected to further processing steps during conversion, such as the thermally initiated crosslinking of organic peroxides (e.g. a PEX-A process), the introduction of catalysts for promote condensation reactions, such as silane crosslinking reactions (eg, PEX-B process) or radiation-induced crosslinking reactions (eg, PEX-C process). These optional modifications allow the production of at least partially biological (renewable) versions of the full range of polymer materials of fossil origin, in particular PE and/or PP materials, and other materials and objects derived from these polymer materials.

Polymers formed in the polymerization process, or polymeric material derived from polymers formed as described above, can be converted or formed into parts or finished products by multiple processes such as extrusion processes for films, sheets, fibers , pipes, profiles, wires and cables, injection molding, hot melt spinning, blow molding or extrusion blow molding, rotational molding, hot dip deposition, calendering, compression, chemical and/or physical foaming processes, or others. Polymer material derived from polymers formed in polymerization processing can be used as a direct substitute for fossil-based polymer materials in these conversion processes. The polymeric material derived from the polymers formed in the polymerization process may optionally be blended with other types of polymers, fillers, additives or combinations thereof and may optionally be included in composite materials or multilayer structures with other materials, such as other polymeric materials, e.g. polypropylene, polyvinylidene chloride, polyesters, ethylenedinyl alcohol, fossil based aluminum etc.

The parts or finished products described above can be used in a variety of applications. For example, these parts or end products can be used in packaging applications including food and non-food packaging, flexible packaging, heat-sealed packaging, thin-wall packaging, transparent packaging, dangerous goods packaging , packaging for detergents and personal care products, packaging for surfactants, etc. These parts or end products can be used in consumer goods applications such as caps and closures, toys, bottles, watering cans, appliances, technical parts, cases, cartridges, hobby products , household items, panels and profiles, covers, shoe insoles, pipe clamps, car trunk/box liners, brooms, caps, ink cartridges, flippers, brushes, bins collectors for punches, seals, handles, garden furniture, household items, thin-walled injection molded parts, co-injection molded parts, food containers, reusable containers, luggage, ice cream containers, dairy containers, cups, containers high impact, high rigidity containers, DVD boxes etc. These parts or end products can be used in automotive applications, such as parts and assemblies for exterior, interior, underhood, underhood, bumpers, body panels, wheel covers, fascias, dashboards, door skins, air conditioning or cooling systems, intake blocks or battery boxes, dashboards or soft touch controls, air bag covers, moldings in the roof pillars, under the belt or hoses, waterproof joints, anti-vibration systems, underbody or side panels, dashboards, structural parts, etc.

These parts or end products can be used in wire and cable applications, such as insulation, sheathing or semiconductor materials for extra high, high and medium voltage alternating current power transmission and distribution. or continuous, data or communication cables or sheaths, building wires or cables, automotive wires or cables, photovoltaic encapsulants, etc. These parts or end products can be used in piping applications such as multilayer pipes, pressure pipes, gas pipes, drinking water pipes, industrial pipes, sewage or sewage pipes. , internal plumbing or heating pipes, single or multi-layer onshore or offshore coatings for oil and gas pipelines, sandless delivery pipes, pipes without deep installation, fittings and relinings, tubing corrugated industrial fittings, mechanical seal compression fittings, solar heat collectors, etc. These parts or end products can be used in film applications, such as heavy duty bags, pouches, trash bags, carrier bags, agricultural films, building or construction films, shrink films heavy duty, grouping shrink films, thin shrink films, form fill seal (FFS) films or bags, sanitary ware films, freezer films, sanitary films, embossed release films , release films, label films, adhesive films, surface protection films, bonding films, cereal packaging, silicone films, stretch films etc.

These parts or finished products can be used in fiber applications, such as non-woven or engineered fibers, continuous filament, filament yarn, raffia, tape, strapping netting, loose fiber, etc.

Other applications in which said parts or end products can be used are, for example, extrusion coating, hot melt adhesives, tie-coat adhesives, medical applications, roofing and waterproofing membranes, carpets , rubberized surfaces, synthetic turf, base resin for masterbatches and compounding.

Carbon atoms of renewable origin contain a higher number of isotopes !*C than carbon atoms of fossil origin.

It is therefore possible to distinguish between a carbon compound derived from a renewable feedstock (of biological origin) and carbon compounds derived from a fossil feedstock (of fossil origin) by analyzing the ratio of the isotopes '° C and 14C.

Thus, a particular ratio of said isotopes can be used as a "tag" to identify a renewable carbon compound and differentiate it from non-renewable carbon compounds.

The isotope ratio does not change during chemical reactions.

Therefore, the isotope ratio can be used to identify compositions of renewable isomeric paraffins, renewable hydrocarbons, renewable monomers, renewable polymers, and materials and products derived from these polymers, and to distinguish them from non-renewable fillers and products.

EXAMPLES The following examples are provided to better illustrate the claimed invention and should not be construed as limiting the scope of the invention. To the extent that specific materials are mentioned, it is for illustrative purposes only and is not intended to limit the invention. Steam cracking experiments illustrating certain embodiments of the present invention have been performed on laboratory equipment. The main parts of the steam cracking unit, the analytical equipment and the calibration procedure used in these examples have been described in detail in the following publications: K.M. Van Geem, S.P. Pyl, M.F. Reyniers, J. Vercammen, J. Beens, G.B. Marin, On-line analysis of complex hydrocarbon mixtures using comprehensive two-dimensional gas chromatography, Journal of Chromatography A. 1217 (2010) 6623-6633 and J.B. Beens, U. A. T. Comprehensive two-dimensional gas chromatography - a powerful and versatile technique. Analyst. 130 (2005) 123-127. Two different compositions of renewable isomeric paraffins P1 and P2, as well as mixtures of said compositions of renewable isomeric paraffins and fossil naphtha N1 have been studied as feedstocks for steam cracking. In addition, as comparative examples, fossil naphtha N1, a third isomeric renewable paraffin composition P3 and a mixture of the third isomeric renewable paraffin composition and fossil naphtha N1 were studied as steam cracking feeds. The laboratory equipment is described with reference to FIG. 1. The feed section controls the feed of steam cracker feed and water from tanks 1 and 2, respectively, to reactor coil 3. Liquid flow was regulated by Coriolis flowmeter controlled pumps 4 (Bronkhorst, The Netherlands) fitted with Bronkhorst"M CORI-FLOWTM series mass flowmeters to provide high accuracy: +0.2% of reading.

CORI-FLOWTM mass flowmeters use an advanced Coriolis-type mass flowmeter to achieve reliable performance even under changing operating conditions such as pressure, temperature, density, conductivity and viscosity.

The pumping frequency was adjusted automatically by the CORI-FLOWTM flow meter controller.

The mass flow, which unlike the volume flow is not influenced by changes in temperature or pressure, of all feeds was measured every second, i.e. almost continuously.

The steam was used as a diluent and heated to the same temperature as the evaporated feed.

Feedstock and steam are heated in electrically heated furnaces 5 and 6, respectively. Downstream of furnaces 5 and 6, feedstock and steam are mixed in an electrically heated furnace 7 filled with quartz balls, allowing efficient mixing and uniformity of feed and diluent before entering the reactor coil 3.

The mixture of feed and dilute vapor enters the reactor coil 3 placed vertically in an electrically heated rectangular furnace 8. Eight thermocouples T positioned along the axial coordinate of the reactor measure the temperature of the process gases at different positions.

The rectangular oven 8 is divided into eight separate sections which could be controlled independently to establish a specific temperature profile.

The pressure in reactor coil 3 is controlled by a back pressure regulator (not shown) placed downstream of the reactor coil 3 outlet.

Two pressure transducers (not shown), placed at the inlet and outlet of the reactor, indicated the coil inlet (CIP) and outlet pressure (COP) respectively.

At the reactor outlet, nitrogen was injected into the reactor effluent as an internal standard for analytical measurements and to some extent contributed to the quenching of the reactor effluent.

The reactor effluent was sampled online, i.e. during the operation of the steam cracker, at an elevated temperature (350°C). Namely, through a valve-based sampling system and uniformly A gaseous sample of the reactor effluent was injected into a two-dimensional gas chromatograph (GC x GC) 9 coupled to a detector flame ionization (FID) and mass spectrometer (MS) using a valved sampling system and uniformly heated transfer lines.

A 6-port, 2-way high-temperature sampling valve of the valve-based sampling system was placed in a furnace, where the temperature was maintained above the dew point of the effluent sample .

Further downstream, the reactor effluent was cooled to about 80°C.

Water and heavier condensates (pyrolysis gasoline (PyGas) and pyrolysis fuel oil (PFO)) were removed by means of a disposal vessel and cyclone 10, while the rest of the effluent was sent straight into a vent.

Before reaching the vent, a fraction of the effluent was taken for analysis on a Refinery Gas Analyzer (RGA) 11. After removal of all remaining water using a water-cooled heat exchanger and a dehydrator, this effluent fraction was automatically injected into Refinery Gas Analyzer (RGA) 11 using an integrated gas sampling valve system (80°C ). The compositions of the renewable isomeric paraffin compositions, namely P1, P2 and P3, were analyzed by gas chromatography (GC). Samples of the composition of renewable isomeric paraffins were analyzed as such, without any pretreatment.

The process is suitable for C2-C36 hydrocarbons. N-paraffins and isoparaffin groups (C1-, C2-, C3- and =C3-substituted) were identified by mass spectrometry and a mixture of known n-paraffins in the C2-C36 range. The chromatograms were divided into three groups of paraffins (C1-

, C2-/C3- and 2 C3 — substituted isoparaffins/n-paraffin) by integrating the groups in the base chromatogram just after the n-paraffin peak. N-paraffins were separated from =C3-substituted isoparaffins by tangential integration of the n-alkanic peak from valley to valley and compounds or groups of compounds were quantified by normalization using a relative response factor of 1.0 at all hydrocarbons. The limit of quantification for each compound was 0.01% by weight. GC settings are shown in Table 1. Table 1. Settings for GC determination of n- and i-paraffins.

PI Injection Split/splitless type injector Split 80 : 1 (Injection volume 0.2pL) Column DBTM-5 (length 30m, i.d. 0.25m, phase thickness Carrier gas 0.25um) He detector Ionization detector program (FID) GC 30°C (2min) - 5°C/min - 300°C (30min), constant flow (1.1mL/min) The results of the analysis are summarized in Table 2 and the detailed results are presented in Tables 3, 4 and 5, respectively. For paraffins in the range C2-C10 of the number of carbon atoms, the amount in % by weight of n-paraffins and the amount in % by weight of total i-paraffins (total i-paraffins), based on the total weight of paraffins in the composition of renewable isomeric paraffins, were determined. For paraffins having a carbon number of C11 or more, the quantities in % by weight, relative to the total weight of the paraffins in the composition of renewable isomeric paraffins, n-paraffins, monobranched i-paraffins, di-i-paraffins - and tribranched and i-paraffins with more than three branches have been determined.

The cloud point of each composition of renewable isomer paraffins P1, P2 and P3 was measured according to standard ASTMD7689-17. The results are presented in Table 2. Table 2. Summary of the compositions of renewable isomer paraffins P1, P2 and 3. Point | Total iP | iP (>sort) | iP (>sort)/Total | % by weight iP of % in % in iP in the turbid interval | weight weight C14-C18 of (°C) number of carbon atoms P3 -48 94.81 15.77 0.17 79.37 men | LA (ææ |mæ on 88 A |E me Ee um (ss P1 comprises, based on the total weight of paraffins in P1, about 31% by weight n-paraffins and about 69% by weight i-paraffins.

The total amount of paraffins in P1 is about 99% by weight of the total weight of P1. Said paraffins were in the C6-C24 carbon number range, and approximately 95% by weight of these paraffins were in the C14-C18 carbon number range.

Of the i-paraffins, about 95% by weight was also in the C14-C18 carbon number range.

P1 comprises, based on the total weight of the paraffins, about 53% by weight of monomethyl-substituted isoparaffins, about 12% by weight of di- and triethyl-substituted and about 3% by weight of isoparaffins with more than three methyl branches .

Table 3. Composition composition of P1 renewable isomer paraffins.

PR iP (total) | iP (mono) | iP (diet | iP (>tri) of sort)

ee 1 1 2 | 00 | 806 | || 3 | 60 | 000 | | | + | 60 | 000 | | | 000 | 806 | || 8 | 60 | 008 | || LU O7 MM | 021 | || 8 | 914 | 988 | OR + (uw (08 | | | De (em 10w | A | 65 | 98 | 08 | o6 | 9 [7 (es (0 | 8th | 0m | Ge B | 0m | 0æ | em | 07 | 0 =| 0m | Ga | ee | 0m | 0.8 | 601 | 004 | 008 | 001 | 000 | 2 | 601 | 0.06 | 0.04 | 0.01 | 00 | 28 | 60 | 000 | 00 | 00 | 0.00 625-029 | 00 | 08 | | | me 0m JR | | | | 5686 | 000 | 0.00 | | [and | 306 | ms | 6260 | 72.10 | 288 P2 includes, based on the total weight of paraffins in P2, about 7% by weight of n-paraffins and about 93% by weight of i-paraffins The total amount of paraffins in P2 is about 100% by weight of the total weight of P2, said paraffins are in the C4-C36 carbon number range, and of said paraffins, about 92% by weight are in the C14-C18 carbon number range. 92% by weight is also in the C14-C18 range of carbon atoms P2 comprises, based on the total weight of the paraffins, approximately 38% by weight of monomethic isoparaffins yl-substituted, about 42% by weight di- and triethyl-substituted and about 10% by weight isoparaffins with more than three methyl branches. Table 4. Composition of P2 renewable isomer paraffins.

| iP (Total) | iP (mono) | iP (di and iP(>tri) of atom tri) of carbon 2? | 000 | 000 | || 3 | 80 | 000 | | | A | 001 | 000 | || 5 | 002 | 001 | || | 8 | 608 | 00 | | | 7 | 009 | 02 | || 8 | 026 | 081 | || [> [ej | | | eea A (08 | 0e | Ge | 07 | 0m [+4 | 08 | 7 | 0æ | Be | 0m | a | em | om | 0m | 0m | 0 | a [on | te | [os | | em | om | om | 0m | on | een om | 0æ | | | mee] om | er | | | [> | om jam | | | Tot | 7 | ee EEK The comparative P3 includes, based on the total weight of paraffins in P3, about 5% by weight of n-paraffins and about 95% by weight of i-paraffins.

The total amount of paraffins in P3 is about 975% by weight of the total weight of P3. These paraffins were in the C4-C36 carbon number range, and approximately 78% by weight of these paraffins are in the C14-C18 carbon number range.

Of the i-paraffins, about 79% by weight are in the C14-C18 carbon number range.

P3 comprises, based on the total weight of the paraffins, about 29% by weight of monomethyl-substituted isoparaffins, about 41% by weight of di- and triethyl-substituted and about 16% by weight of isoparaffins with more than three branches methyl.

Table 5. Composition of P3 renewable isomer paraffins (comparative examples).

PB iP (Total) | iP (mono) | iP (di and iP(>tri) of atom tri) of carbon za 0 |. | | _LU$ | 000 | 000 | || A | 001 | 001 | || (oæ em | | | 8 | 006 | 090 | || 1 O7 | 018 | 039 | || | 8 | 88 | 181 || 9 | 044 | 882 | || | 036 | 829 | || MM | 028 | 202 | 035 | 1.66 | 000 aw | 0m | 08 | 0m | 07 | 08 | [> | 9th | oe | 00 | 0m | 0m _ | æ | 0 | 0w | 0æ | 0æ | 0m |

[> [eme [0e L om | om am 1 | SN | 00 | om | 0m [90 | em | em | em | 0m es om er | | | mas em jam |. | | ow jam jm | | | [er | 56 | a | mm | | The PiONA (paraffins, isoparaffins, olefins, naphthenes, aromatics) composition of the fossil naphtha N1 used in the examples and in the comparative examples was determined by gas chromatography coupled with a flame ionization detector (GC-FID). The results of the analysis are presented in Table 6.

Ni included hydrocarbons in the C4-C7 carbon number range, or about 99 wt% of the total weight of N1. N1 comprises about 34% by weight of n-paraffins, about 40% by weight of i-paraffins and about 25% by weight of mono naphthenes relative to the total weight of N1.

Table 6. Composition of fossil naphtha N1.

ME Mono Atom Number of Carbon Naphthenes [> pe | em [um 1 > i [eæ [om [+ #7 a | + 8 85 8m |. @ 6 60 1000

|. @ 000 906 [000 5010 600 Jow 000 Two mixtures B1 and B2 of N1 and P1 and P2, respectively, were formed. For the comparative examples, a B3 mixture of N1 and P3 was formed. The compositions of mixtures B1-B3 are presented in the table

7.

N1 comprises 250 ppm by weight sulfur. All P1-P3 Renewable Isomeric Paraffin compositions are initially substantially sulfur free and contain less than 1 ppm by weight sulfur. When used as unblended feed for steam cracking, Pl and P2 were added dimethyl sulfide (DMDS) to contain 250 wppm sulfur, i.e. to match the sulfur content of the N1. Blend B2 was also added to DMDS to contain 250 wppm sulfur. The unmixed P3 and the B1 and B3 mixtures were not added.

Therefore, the unblended P3 was essentially sulfur free, while the sulfur content of the B1 and B3 blends came from N1 and was 65.2 ppm by weight. Therefore, 250 wppm sulfur was added to P1 and P2 respectively, and 187.5 wppm sulfur was added to B2 which already included 65.2 wppm sulfur from N1.

The DMDS was added to the charge in the vapor. In other words, the sulfur addition was done by adding DMDS to the steam and then injecting the steam into the steam cracking furnace (reactor coil 3) to achieve a sulfur content of 250 mg sulfur/kg feed. The feeds and their sulfur content are summarized in Table 7.

Table 7. Composition and sulfur content of mixtures B1, B2 and B3.

Filling Composition Sulfur (ppm OT ee [+ eee | | € | eee | 75% by weight | 25% by weight 62.5 ie 75% by weight | 25% by weight 250 ee B3 (comparative) | 75% by weight | 25 wt% 62.5 EE 1e Steam cracking of the feeds described above was carried out at three different coil outlet temperatures (TOCs), 800°C, 820°C and 840°C. flow rate between water and feed (dilution) was kept constant at 0.5 g H20 / g feed Table 8 shows the average amounts in % by weight of CO, CO: and C2H2 impurities measured from steam cracking effluent at different coil outlet temperatures Percent by weight is based on the total weight of the steam cracking effluent Total impurities are the sum of the amounts in weight % of CO, CO: and C2H2 (total amount of CO, CO: and C2H2) Table 8. Average weight percentage of CO, CO: and C2H2 impurities in the steam cracking effluents obtained at the different TOCs. Load co CO2 C2H2 Impurities

IN

N1 0.015 0.008 0.239 0.262 meas LL LE | we | a | 00 THE 0 | em | 0 | 0 | P3 0.061 0.010 0.593 0.664 men LL LE pr | 07 | in | Da | 08 m2 | me | om | Dam | Gas B3 0.074 0.027 0.848 0.949

PI As can be seen in Table 8, it is surprising to find that the compositions of renewable isomeric paraffins and mixtures comprising renewable isomeric paraffin compositions have a higher percentage by weight of total impurities than fossil naphtha. However, as can be seen in Table 8, P1 and P2, as well as their mixtures B1 and B2, form much less total impurities than P3 and its mixture B3.

The combination of fossil naphtha with a composition of renewable isomeric paraffins increased the production of CO and CO2. This can be seen for example by comparing P1 and B1, as well as P3 and B3 in Table 8. It should be noted that the production of CO and COz increased significantly when P3 was mixed with N1 (this is i.e. P3 versus B3) despite increasing the sulfur content of the feed from less than 1 wppm to 62.5 wppm. On the other hand, comparing P1 and B1 (Table 8), a much more subtle increase in the production of CO and CO: was recorded despite the decrease in the sulfur content of the feed from 250 ppmw to 62.5 ppm by weight. The addition of the mixture with DMDS helped to decrease the production of CO and CO2, as can be seen by comparing P2 and B2 with P1 and B1 (Table 8). Overall, it can nevertheless be concluded that the reduction in the ratio of the amount in % by weight of isoparaffins with more than three branches to the total weight percentage of isoparaffins in the composition of renewable isomeric paraffins considerably reduces the formation of CO and above all of CO”. This effect can be demonstrated in particular by comparing B1 and B3 (Table 8) containing the same amount of sulfur. It can also be concluded that an increase in the amount of isoparaffins in % by weight in the interval C14-C18 of the number of carbon atoms of the composition of renewable isomeric paraffins also contributes to the reduction in the formation of CO and of CO”.

As shown in Table 8, the fossil naphtha produced surprisingly less C2H2 than either the Renewable Isomeric Paraffin composition or the blends comprising the Renewable Isomeric Paraffin composition. Surprisingly, the production of C2H2 increased when the renewable isomeric paraffin compositions were combined with fossil naphtha, respectively, as can be seen by comparing P1 with B1, P2 with B2, and P3 with B3 (Table 8). Sulfur content has no significant influence on C2H2 production during steam cracking. As shown in Table 8, P2 generated slightly more C2H2 than P1. However, comparing P3 with P1 and P2, we see that P3 generated much more C2H2 than P1 or P2 (Table 8). This is surprising considering the difference in degree of isomerization between P2 and P3 (2.29 percentage points) and the difference in degree of isomerization between P1 and P2 (23.48 percentage points). It can therefore be concluded that the degree of isomerization is not a main factor in controlling the formation of C2H2. Similarly, as shown in Table 8, the increase in C2aH2 production between B1 and B2 was much more subtle than the increase in C2H2 production between B3 and B1 or B2, with B1 producing less C2H2 than B2. or B3, and B2 producing less C2H2 than B3. It can therefore be concluded that decreasing the ratio of the amount in % by weight of isoparaffins with more than three branches to the amount in % by weight of total isoparaffins in the composition of renewable isomeric paraffins decreases the formation of C:H2. In addition, increasing the amount in % by weight of isoparaffins in the range C14-C18 of the number of carbon atoms in the composition of renewable isomeric paraffins contributes to reducing the formation of C2H2. Therefore, the wt% of total impurities is also decreased by decreasing the ratio of the wt% amount of isoparaffins with more than three branches to the total wt% amount of isoparaffins in the paraffin composition. renewable isomers. This effect can be further enhanced by increasing the amount in % by weight of isoparaffins in the range C14-C18 of the number of carbon atoms in the composition of renewable isomeric paraffins. Tables 9 to 12 present more detailed analysis results of steam cracking effluents. As can be seen in Tables 11 and 12, steam cracking performed at TOC 800°C and 820°C produced less CO and CO2 than steam cracking performed at TOC 840°C. This was observed for all the loads of the examples, namely P1, P2, B1 and B2. A particularly low production of CO and CO2 was obtained for all the charges of the examples (P1, P2, B1 and B2) at TOC 800°C.

Surprisingly, COT 820°C increased CzHz formation when the feed was P1 or P2 compared to steam cracking of the same feed at COT 800°C and 840°C. This effect was not observed with steam cracking mixtures B1 and B2. C2He2 production decreased with TOC when the feed was B1 or B2. The lowest C2Hz production was obtained at TOC 800°C for all the loads of the examples (P1, P2, B1 and B2). Consequently, the production of CO, CO: and C2H2 impurities further decreased at 800°C TOC. When steam cracking mixtures of fossil naphtha and P1 or P2, a TOC between 800 and 820°C has been shown to decrease the production of CO, CO: and C2Hz impurities compared to TOC 840° vs. Table 9. Analysis of steam cracking effluents, feeds N1 and P3 (comparative examples). The results are expressed in % by weight based on the total weight of effluent.

Dilution 0.5 0.5 0.5 0.5 0.5 0.5 (gH20/g me Non- 36.733 | 24.735 | 17.024 | 14.622 | 8.228 | 4.678 aromatic C5-C9 BTX 2.699 | 6.020 | 7.124 | 5.301 9.699 |12.815 eeen [OO toluene, mes ||LL Ethene and |35.607 |41.018 |45.116 |46.354 |48.313 |48.948

EE LL HVC (ethene, | 41,879 | 51,461 | 57,203 | 58,065 | 64,846 | 68,571 propene, 1,3-butadiene, and BTX) Impurities 0.259 | 0.196 | 0.533 | 0.560 | 0.671 0.760 total (CO, CO2, and C2H2) Impurities 100.00 | 100.00 | 100.00 | 100.00 | 100.00 | Table 10, Analysis of Steam Cracking Effluents, Feed B3 (Comparative Examples). The results are expressed in % by weight based on the total weight of effluent.

Dilution (gH20/g 0.5 0.5 0.5 om LL

Non-aromatic 19.625 10.231 7.692 se BTX (benzene, 5.252 8.499 10.933 kun na HVC (ethene, 52.549 63.521 66.286 propene, 1,3- butadiene, and BTX) Total impurities 1.216 0.752 0.752 0.879 and total impurities Lt CO20.9 (CO, 0.879 Table 11. Analysis of Steam Cracking Effluent, Raw Materials P1 and P2 Results are expressed as % by weight based on total weight of effluent.

8.890 10.256 9.937 12.528 | ) 45.228 50.844 51.536 46.869 | 48.227 | 47.531 Mae LEE HVC

Total impurities 0.218 0.752 0.649 0.427 0.668 0.553 (CO, and LI Total impurities 100.00 100.00 100.00 100.00 | 100.00 | 100.00 of all Table 12. Analysis of steam cracking effluents, Loads B1 and B2 The results are expressed in % by weight based on the total weight of the effluent.

Dilution 0.5 0.5 0.5 0.5 0.5 0.5 (gH20/g charge) No- 15.081 15.582 12.825 20.136 | 14,722 | 10.847 aromatic Fa

BTX (benzene, 5.684 7.355 7.342 5.860 8.033 10.097 toluene, xylenes) ethene and | 44.572 49.868 51.457 45.913 | 45,573 | 48.257 stinks HVC LE (ethene, | 55.845 63.611 65.436 57.751 | 59.717 | 64.667 propene, 1,3- butadiene, and BTX) Total impurities 0.348 0.354 1.023 0.453 0.677 0.834 100.01 103.65 | 100.00 | 100.00 total of all species The practice and practice of the present invention is further discussed in the following numbered clauses:

1. A process comprising the steps of a) providing a thermal cracking charge comprising 1 to 100% by weight of isomeric renewable paraffin composition based on the total weight of the thermal cracking charge, the renewable isomeric paraffin composition comprising at least 60% by weight of paraffins relative to the total weight of the composition of renewable isomeric paraffins, where 10 to 95% by weight of said paraffins are isoparaffins, and the ratio of the amount in% by weight of isoparaffins with more than three branches in total amount in % by weight of the isoparaffins is less than 0.15, and 0 to 99 % by weight of fossil naphtha relative to the total weight of the thermal cracking charge, the sum of the amounts in % by weight of the composition renewable isomeric paraffins and fossil naphtha representing at least 90% by weight of the total weight of the thermal cracking charge; and b) thermally cracking the thermal cracking charge supplied in step a) to form a cracking product comprising a mixture of hydrocarbons.

2. Process according to clause 1, wherein the thermal cracking charge comprises 50 to 100% by weight of renewable isomeric paraffin composition based on the total weight of the thermal cracking charge, and 0 to 50% by weight of fossil naphtha relative to the total weight of the thermal cracking charge.

3. Process according to any one of the preceding clauses, in which the thermal cracking charge comprises 50 to 85% by weight of composition of renewable isomeric paraffins and 15 to 50% by weight of fossil naphtha, preferably 60 to 85% by weight of composition of renewable isomeric paraffins and 15 to 40% by weight of fossil naphtha, more preferably 70 to 85% by weight of composition of renewable isomeric paraffins and 15 to 30% by weight of fossil naphtha, relative to the total weight of the thermal cracking charge, the sum of the amounts in % by weight of the composition of renewable isomeric paraffins and of the fossil naphtha preferably representing at least 95% by weight, preferably at least 99% by weight, relative to the total weight of the thermal cracking load.

4. Process according to any one of the preceding clauses, in which the ratio of the quantity in % by weight of isoparaffins with more than three branches to the total quantity of % by weight of the isoparaffins in the composition of renewable isomeric paraffins is lower to 0.12, preferably less than 0.10, more preferably less than 0.05.

5. Process according to any one of the preceding clauses, in which, among the isoparaffins of the composition of renewable isomeric paraffins, at least 80% by weight, preferably at least 85% by weight, more preferably at least 90% by weight , even more preferably at least 95% by weight, are in the range C14-C18 by the number of carbon atoms.

6. Process according to any one of the preceding clauses, in which, among the paraffins of the composition of renewable isomeric paraffins, 60 to 95% by weight, preferably 60 to 80% by weight, and more preferably 65 to 70% by weight are isoparaffins, the renewable isomeric paraffin composition comprising paraffins preferably at least 70% by weight, more preferably at least 80% by weight, more preferably at least 90% by weight, even more preferably at least 95% by weight , relative to the total weight of the composition of renewable isomeric paraffins.

7. Process according to any one of the preceding clauses, in which the fossil naphtha comprises 20 to 85% by weight of paraffins, 0 to 35% by weight of olefins, 10 to 30% by weight of naphthenes and 0 to 30% by weight of aromatic compounds relative to the total weight of the fossil naphtha, the percentage by weight of hydrocarbons in the fossil naphtha preferably being at least 95% by weight, more preferably at least 99% by weight relative to the total weight of the fossil naphtha .

8. Process according to any one of the preceding clauses, in which the thermal cracking charge comprises 20 to 300 ppm by weight of sulphur, preferably 20 to 250 ppm by weight, more preferably

20 to 100 ppm by weight, and even more preferably 50 to 65 ppm by weight.

9. Process according to any one of the preceding clauses, in which step b) is carried out at a coil outlet temperature (COT) selected from the range of 780°C to 890°C, preferably 800°C. C to 860°C, more preferably 800°C to 840°C, and even more preferably 800°C to 820°C. 10, Process according to any one of the preceding clauses comprising the step consisting in c) subjecting at least a part of the cracking product formed in step b) to a purification treatment in order to eliminate at least one of the compounds among CO, CO2 or C2H2.

11. Process according to any one of the preceding clauses comprising the step consisting in d) subjecting at least a part of the cracking product formed in step b), or at least a part of the cracking product subjected to the purification treatment of step c), or both, to a polymerization treatment to produce polymers.

12. A process according to any preceding clause, comprising the steps of providing multiple thermal cracking furnaces, and performing step b) in at least one of the multiple thermal cracking furnaces.

13. Process according to clause 12, comprising the steps of obtaining cracked products from the multiple thermal cracking furnaces, and mixing the obtained cracking products to form a combined cracking product, and optionally, subjecting at least a part cracking product combined with a purification treatment to remove at least one of CO, CO2 or C2Hz, or a polymerization treatment to form polymers, or both the purification treatment and the polymerization treatment.

14. A thermal cracking batch comprising 1 to 100% by weight of renewable isomeric paraffins composition based on the total weight of the thermal cracking batch, the renewable isomeric paraffins composition comprising at least 60% by weight of paraffins based on the weight total composition of renewable isomeric paraffins, wherein from 10 to 95% by weight of said paraffins are isoparaffins and the ratio of the amount in% by weight of the isoparaffins with more than three branches to the total amount of percentage by weight of the isoparaffins is less than 0.15; and 0 to 99% by weight of fossil naphtha based on the total weight of the thermal cracking charge, the sum of the quantities in % by weight of the composition of renewable isomeric paraffins and the fossil naphtha representing at least 90% by weight of the weight total thermal cracking load.

15. Thermal cracking charge according to clause 14, wherein the thermal cracking charge comprises 50 to 100% by weight of the composition of renewable isomeric paraffins based on the total weight of the thermal cracking charge, and 0 to 50% by weight of fossil naphtha relative to the total weight of the thermal cracking charge.

16. A thermal cracking charge according to clause 14 or 15, wherein the thermal cracking charge comprises 50 to 85% by weight of renewable isomeric paraffin composition and 15 to 50% by weight of fossil naphtha, preferably 60 to 85% by weight of renewable isomeric paraffin composition and 15 to 40% by weight of fossil naphtha, more preferably 70 to 85% by weight of renewable isomeric paraffin composition and 15 to 30% by weight of fossil naphtha based on the total weight of the thermal cracking charge, the sum of the amounts in % by weight of the composition of renewable isomeric paraffins and of the fossil naphtha being preferably at least 95% by weight, more preferably at least 99% by weight, of the total weight thermal cracking load.

17. Thermal cracking charge according to any one of the preceding clauses 14 to 16, in which the ratio of the quantity in % by weight of isoparaffins with more than three branches to the quantity in % by weight of the total isoparaffins in the composition of renewable isomeric paraffins is less than 0.12, preferably less than 0.10, more preferably less than 0.05.

18. Thermal cracking charge according to any one of the preceding clauses 14 to 17, in which among the isoparaffins in the composition of renewable isomeric paraffins, at least 80% by weight, preferably at least 85% by weight, more preferably at least at least 90% by weight, even more preferably at least 95% by weight, is in the range of C14-C18 of the number of carbon atoms.

19. Thermal cracking charge according to any one of the preceding clauses 14 to 18, in which among the paraffins of the composition of renewable isomeric paraffins, 60 to 95% by weight, preferably 60 to 80% by weight, more preferably 65 -70% by weight are isoparaffins, the composition of renewable isomeric paraffins comprising paraffins preferably at least 70% by weight, more preferably at least 80% by weight, more preferably at least 90% by weight, even more preferably at least 99% by weight, of the total weight of the composition, of renewable isomeric paraffins.

20, Thermal cracking charge according to any one of the preceding clauses 14 to 19, wherein the fossil naphtha comprises 20 to 85% by weight paraffins, 0 to 35% by weight olefins, 10 to 30% by weight naphthenes and 0 to 30% by weight of aromatic compounds based on the total weight of the fossil naphtha, the percentage by weight of the hydrocarbons in the fossil naphtha being preferably at least 95% by weight, more preferably more than 99% by weight based on total weight of fossil naphtha.

21. A thermal cracking charge according to any of the preceding clauses 14 to 20, wherein the thermal cracking charge comprises 20 to 300 ppm by weight of sulfur, preferably 20 to 250 ppm by weight, more preferably 20 to 100 ppm by weight, and even more preferably 50 to 65 ppm by weight.

22. A cracked product comprising a mixture of hydrocarbons obtainable by a process according to any one of the preceding clauses 1 to 13, in which the sum of the quantities in % by weight of CO, CO: and C2H2 in the product of cracking is less than 1.5% by weight, preferably less than 1.3% by weight, more preferably less than 1.1% by weight, even more preferably less than 0.8% by weight, relative to the total weight of the cracking product.

23. Use of cracking product according to Clause 22 to produce polymers such as polypropylene, polyethylene, or both.

24. Manufactured article comprising polymers obtainable by a process according to clause 11 or clause 13.

The foregoing description has provided, by way of non-limiting examples of applications and particular embodiments of the invention, a complete and informative description of the best mode currently envisaged by the inventors for carrying out the invention. However, it is clear to those skilled in the art that the invention is not limited to the details of the embodiments presented in the foregoing, but that it can be implemented in other embodiments by equivalent means or in different combinations. of achievements without departing from the characteristics of the invention.

Further, some of the features of the embodiments of this invention disclosed above may be used to their advantage without the corresponding use of other features.

As such, the foregoing description should be considered a mere illustration of the principles of the present invention, and not a limitation thereof.

Accordingly, the scope of the invention is limited only by the appended patent claims.

Claims (8)

Claims 1. A thermal cracking charge comprising 1 to 100% by weight of renewable isomeric paraffins composition based on the total weight of the thermal cracking charge, the renewable isomeric paraffins composition comprising at least 60% by weight of paraffins based on the weight total composition of renewable isomeric paraffins, wherein from 10 to 95% by weight of said paraffins are isoparaffins and of said isoparaffins, at least 80% by weight are in the range of C14-C18 by the number of carbon atoms, and the ratio of the amount in % by weight of the isoparaffins with more than three branches to the total amount of % by weight of the isoparaffins is less than 0.12; and 0 to 99% by weight of fossil naphtha based on the total weight of the thermal cracking charge, the sum of the quantities in % by weight of the composition of renewable isomeric paraffins and the fossil naphtha representing at least 90% by weight of the weight total thermal cracking load. 2. A thermal cracking charge according to claim 1, wherein the thermal cracking charge comprises 50 to 100% by weight of renewable isomeric paraffin composition based on the total weight of the thermal cracking charge, and 0 to 50% by weight of fossil naphtha relative to the total weight of the thermal cracking charge. 3. Thermal cracking charge according to claim 1 or 2, in which the thermal cracking charge comprises 50 to 85% by weight of composition of renewable isomeric paraffins and 15 to 50% by weight of fossil naphtha, preferably 60 to 85% by weight of renewable isomeric paraffin composition and 15 to 40% by weight of fossil naphtha, more preferably 70 to 85% by weight of renewable isomeric paraffin composition and 15 to 30% by weight of fossil naphtha based on the total weight of the thermal cracking charge, the sum of the amounts in % by weight of the composition of renewable isomeric paraffins and of the fossil naphtha being preferably at least 95% by weight, more preferably at least 99% by weight, of the total weight thermal cracking load. 4. Thermal cracking charge according to any one of the preceding claims, in which the ratio of the quantity in % by weight of isoparaffins with more than three branches to the quantity in % by weight of the total isoparaffins in the composition of isomeric paraffins renewable is less than 0.10, preferably less than 0.05. 5. Thermal cracking charge according to any one of the preceding claims, in which among the isoparaffins in the composition of renewable isomeric paraffins, at least 85% by weight, preferably at least 90% by weight, more preferably at least 95% by weight, are in the range of C14-C18 of the number of carbon atoms. 6. Thermal cracking charge according to any one of the preceding claims, in which among the paraffins of the composition of renewable isomeric paraffins, 60 to 95% by weight, preferably 60 to 80% by weight, more preferably 65-70% by weight are isoparaffins, the renewable isomeric paraffin composition comprising paraffins preferably at least 70% by weight, more preferably at least 80% by weight, more preferably at least 90% by weight, even more preferably at least 99% by weight weight, of the total weight of the composition of renewable isomeric paraffins. 7. Thermal cracking charge according to any one of the preceding claims, in which the fossil naphtha comprises 20 to 85% by weight paraffins, 0 to 35% by weight olefins, 10 to 30% by weight naphthenes and 0 to 30% by weight of aromatic compounds relative to the total weight of the fossil naphtha, the percentage by weight of the hydrocarbons in the fossil naphtha being preferably at least 95% by weight, more preferably more than 99% by weight relative to the total weight of the fossil naphtha. 8. Thermal cracking charge according to any one of the preceding claims, in which the thermal cracking charge comprises 20 to 300 ppm by weight of sulphur, preferably 20 to 250 ppm by weight, more preferably 20 to 100 ppm by weight, and even more preferably 50 to 65 ppm by weight.