Catalytic cracking process in a fluidized bed of glycerides for producing high-stability gasoline using a catalyst formulation based on faujasitic zeolite modified by ion exchange with rare earths, and high stability gasoline

Abstract

The present invention relates to a catalytic cracking process in a fluidized bed of glycerides for producing high-stability gasoline, in which a feed stream of vegetable oils and / or animal fat containing glycerides is brought into contact with a catalyst based on faujasitic zeolite modified by ion exchange with rare earth oxides (RE2O3) in high concentrations. The present invention further relates to the gasoline obtained by the aforementioned process, which is 100% renewable.

Description

[0001] Fluidized Bed Catalytic Cracking Process of Glycerides for the Production of High-Stability Gasoline Using a Rare Earth Ion-Exchange Modified Faujasitic Zeolite-Based Catalyst Formulation and High-Stability Gasoline Field of the Invention

[0001] The present invention belongs to the technical field of biofuels derived from biomass conversion using fluidized catalytic cracking (FCC) technology. More specifically, the present invention teaches a fluidized bed catalytic cracking process of glycerides for the production of high-stability gasoline using a high-content ion-exchange modified faujasitic zeolite-based catalyst formulation. Background of the Invention

[0002] Fluidized bed catalytic cracking (FCC) is one of the most widely used processes worldwide for converting heavy hydrocarbon streams into fuels. The process basically consists of breaking carbon-carbon bonds, generating smaller and lighter molecules, mainly in the range of 3 to 12 carbon atoms (liquefied petroleum gas - LPG and gasoline). On a smaller scale, fuel gas (hydrogen, C1-C2), light oils (C3-C4) and decanted products, as well as coke, are produced.

[0003] The search for new raw materials from renewable sources has been encouraged with the aim of reducing dependence on oil and also due to issues related to environmental preservation. In view of this, the use of biomass as a substitute for fossil hydrocarbons in fuel production has grown rapidly in recent years.

[0004] There are numerous examples in the literature of the use of grease streams for renewable fuel production in the FCC.

[0005] Vegetable oils, such as soybean oil and castor oil, or animal fats (triglycerides), such as beef tallow, have been used in FCC because their molecular structure features linear side chains with up to 20 carbon atoms. Figure 1 shows a typical triglyceride structure, with oleic, linoleic, and linolenic acids in its side chains, i.e., linear side chains with 18 carbon atoms, with one, two, or three unsaturations, respectively. Although represented with 18 carbon atoms, the number of carbons in the side chains can typically vary between 9 and 20 in vegetable oils and animal fats.

[0006] When linoleic and linolenic acids are broken down, they generate highly unstable products due not only to the formation of oxygenated compounds, but also of dienes.

[0007] Despite the increasingly widespread use of vegetable oil and animal fat streams in hydroprocessing, the use of these streams in FCC is still limited by difficulties encountered in the process and in adapting the generated products to the stringent specifications of the automotive market worldwide, mainly regarding gasoline stability.

[0008] The quality and stability of gasoline are significantly affected by the presence of conjugated dienes within the triglyceride molecule itself, which are not converted in the cracking reactor. This leads to adverse effects on engine performance, pollutant formation, and compliance with environmental regulations.

[0009] In order to try to solve processing problems, the literature reports the use of various types of catalysts, the best choice of which will always depend on the specific characteristics of the raw material and the desired products. Catalysts with acidic characteristics are widely used in FCC processes with vegetable oils for their transformation into ethene, propene, and aromatics. HZSM-5 zeolite, one of the typical components of the catalysts used, exhibits high activity for this reaction. The acidity, chemical composition, and pore size of the catalyst are among the main characteristics that make HZSM-5 zeolite exhibit good activity for removing oxygen present in the triglyceride. However, there is a large production of gas in the LPG range (C3-C4), especially ethene and propene. In addition, the presence of dienes in gasoline can cause some problems in the use of this fuel.The presence of unsaturated hydrocarbons, primarily conjugated dienes, can significantly decrease gasoline's stability against oxidation. These olefins can react over time, leading to the formation of deposits and gums in the vehicle's fuel system, causing clogging of fuel injectors and other components, reducing engine efficiency and increasing maintenance. Although olefins contribute to gasoline's octane number, they are less effective compared to aromatic hydrocarbons and other components. Gasoline with a lower octane number can cause knocking problems in engines, affecting performance and potentially causing engine damage.

[0010] Therefore, managing these compounds is crucial to ensuring the efficiency and sustainability of modern automotive fuels.

[0011] Patent BR PI 0707890-0 (now expired) addresses a fluid catalytic cracking (FCC) process using a preheated high-boiling-point hydrocarbon feed (paraffins in the presence of triglycerides). Although the document shows an FCC process using triglycerides in the feed, specifically palm or rapeseed oil, the process uses a cracking catalyst comprising a large-pore zeolite (USY) or medium-pore zeolite ZSM-5. Furthermore, the document does not address the problem of naphtha instability when triglycerides are co-processed in catalytic cracking, limiting their content to 50% of the total feed.It is known that higher triglyceride content in co-processing leads to high gum formation, reflected in the current gum assay, and a decrease in fuel stability against oxidation during storage. This can be predicted by the induction period assay, as the conjugated dienes present in the triglyceride side structure are converted in the fluid catalytic cracking reactor into smaller molecules containing these dienes. These highly reactive molecules lead to product instability. This instability is resolved through catalysts with high rare earth content, which promote the conversion of conjugated dienes into aromatics, making the product more stable and with a higher octane number.

[0012] Patent BR PI 8304794-8 (also expired) deals with the processing of vegetable oils in FCC units, but does not address the issue of the stability of the gasoline produced, nor does it mention the use of a catalyst based on faujasitic zeolite modified by ion exchange with rare earths.

[0013] Patent application BR PI 0922136-0 (in the public domain) describes a process for fluid catalytic cracking (FCC) that uses a feedstock comprising a petroleum-based hydrocarbon feed fraction and a biorenewable feed fraction. The document shows several options for vegetable oils used in the FCC process as the biorenewable fraction and uses a cracking catalyst comprising a synthetic faujasite zeolite of type Y such as USY, or a rare earth exchanged faujasite zeolite USY.

[0014] The catalyst for the FCC process proposed in the present invention is substantially different from that proposed in this document BR PI 0922136-0, as it seeks to solve the problem of product stability by establishing a minimum rare earth content in the catalyst in order to convert the conjugated dienes present in the triglyceride used in the feed, which, upon conversion, will produce naphtha without such dienes, in addition to eliminating the presence of oxygen in the naphtha and other products. Another advantage of the catalyst of the present invention lies in meeting the thermal balance of the FCC, since catalysts with higher rare earth contents show a greater tendency to generate the coke necessary to meet the thermal demand of the reactor.

[0015] The catalyst of the present invention differs even further from the catalyst of this document with respect to the zeolite surface area / catalyst matrix surface area ratio, since this document establishes a minimum value of at least 2, while the proposal of the present invention establishes a maximum ratio of 1.

[0016] The international publication WO 2013 / 102662 focuses on obtaining non-gasoline C2-C4e olefins from an FCC feedstock comprising a cellulosic material and a hydrocarbon co-feed. This is achieved using a catalyst combining zeolite Y or ultrastable zeolite Y (USY) with an MFI-type zeolite.

[0017] In the present invention, the use of catalysts with a high rare earth content is essential for the conversion of conjugated dienes present in the glyceride molecule used in food, as the catalyst provides a more stable naphtha (gasoline). This is not the case with ultrastable USY zeolites, which do not contain rare earths.

[0018] Furthermore, the aforementioned document utilizes cellulosic material in the feed stream, whose chemical nature differs substantially from the glyceride (ester) structure used in the present invention, since such cellulosic materials comprise various families of oxygenated compounds, such as ketones, phenolics, aldehydes, and non-ester ethers. These compounds do not contain substantial amounts of compounds with conjugated double bonds (conjugated dienes) and, therefore, do not generate unstable products when converted in the FCC reactor.

[0019] Patent BR 102014003847-7 B1 describes a catalytic system to increase the yield of high-octane gasoline in FCC processes, having as components a beta zeolite and a Y zeolite and a rare earth content between 0.5 and 6.0% w / w, in addition to other ingredients typical of FCC catalysts, such as the active matrix and binders.

[0020] The document in question uses rare earth-modified Y zeolites that can be prepared by ion exchange, where sodium ions, present in the zeolite structure, are exchanged for rare earth cations.

[0021] Exchange solutions typically contain a mixture of rare earth metal salts, such as cerium, lanthanum, neodymium, praseodymium salts, naturally occurring rare earth metals, and mixtures thereof.

[0022] In addition to beta and Y zeolites and rare earth elements, the catalytic system also includes other ingredients typical of FCC catalysts, such as the active matrix, especially those with activity for the generation of hydrocarbons in the gasoline range, such as aluminas and silica-aluminas, the inert matrix (clays, such as kaolin and treated kaolin) and the synthetic matrix, the binder (typically an inorganic oxide sol, such as silica, alumina or silica-alumina, or mixtures thereof).

[0023] The document focuses on the catalytic system and its application to the FCC process using vegetable oils.

[0024] Patent application BR 102020016971-8 teaches how to maximize the generation of BTX aromatics (benzene, toluene, xylenes) from vegetable oils or animal fats, using ZSM-5-based catalysts. Gas production is quite high, always above 20% by weight, in which the total LPG yield can reach up to 30% by weight, too high for catalytic cracking units that do not have propylene separators and, therefore, are unable to commercialize it.

[0025] Therefore, there is no mention in the literature of catalysts capable of maximizing products in the gasoline range that can simultaneously confer good stability through the conversion of conjugated dienes present in the triglyceride molecule.

[0026] In order to solve this problem, the present invention proposes a way to process vegetable oils or animal fats (triglycerides) via a fluidized bed catalytic cracking (FCC) process that allows obtaining high-octane gasoline in order to stimulate the production of renewable fuels to replace fossil hydrocarbons.

[0027] To achieve this result, the present invention proposes a catalyst formulation based on ion-exchange modified faujasitic zeolite with rare earths for application in the processing of glycerides (mono-, di-, or triglycerides) via fluidized bed catalytic cracking units (FBCs). The catalyst formulation used in the cracking process of the present invention produces high-quality, sulfur-free gasoline with high stability due to the conversion of conjugated dienes present in the glyceride molecule through hydrogen transfer reactions provided by the presence of high levels of rare earths in the catalyst. This catalyst exhibits better performance and stability when compared to conventional catalysts of the prior art. Summary of the invention

[0028] The present invention relates to a fluidized bed catalytic cracking (FCC) process of glycerides for the production of highly stable gasoline using a catalyst formulation based on faujasitic zeolite modified by ion exchange with high levels of rare earth elements.

[0029] The present invention also relates to gasoline obtained by the aforementioned process, which is 100% renewable and highly stable since it has a low oxygen, washed gum, and diene content. Brief description of the figures.

[0030] Figure 1 shows the typical molecular structure of a soybean oil with oleic acid chains (top), linoleic acid chains (middle), and linolenic acid chains (bottom). Detailed description of the invention.

[0031] In the FCC process, the reactions take place in a reactor where the catalyst, in the form of solid particles, comes into contact with a feed of vegetable oils and / or animal fat preheated to a suitable temperature, between 100°C and 360°C, and introduced into a reaction zone, resulting in products that contribute to the dispersion of the catalyst particles in the reactor. While promoting deoxygenation and cracking reactions, the catalyst is deactivated by the coke generated as a byproduct of the reactions throughout the reactor.

[0032] The following conditions are considered in the reactor: (i) reaction temperature in the range between 400°C and 520°C, (ii) absolute pressure in the range between 200 and 400 kPa, (iii) catalyst / vegetable oil or animal fat ratio in the range between 3 and 20, and (iv) contact time between reactants and catalyst in the range between 0.5 and 4.0 seconds, which may also be between 1.5 and 3.0 seconds.

[0033] At the reactor outlet, after the deoxygenation and cracking reactions are complete, the deactivated catalyst is separated from the reaction products. The deactivated catalyst then proceeds to a rectification stage where it receives an inert gas stream, preferably water vapor, to remove hydrocarbon products that are then mixed with the already separated products to compose the hydrocarbon streams obtained in the process. After rectification, the deactivated catalyst undergoes a regeneration stage by combustion in the presence of air, resulting in combustion gases and the regenerated catalyst, which returns to the reaction zone at a high temperature, around 700°C, sufficient to provide heat for the endothermic reactions of the process, thus completing one cycle of the process of the present invention.

[0034] The hydrocarbon streams recovered in the process comprise: fuel gas (hydrogen, C1 and C2), light gases (C3 and C4); naphtha (C5+ - 220°C); and other hydrocarbons (>220°C).

[0035] The catalyst used in catalytic cracking (FCC), in general, is composed of several components such as zeolites, an active matrix (aluminas), a synthetic matrix (silicas), and an inert matrix (kaolin) in its chemical composition.

[0036] For informational purposes only, the process for obtaining the FCC catalyst follows a known methodology described in publication WO 2006 / 067154. First, a suspension is prepared containing the components kaolin, zeolites, a low-sodium silica source stabilized with ammonia, microcrystalline boehmite alumina, and pseudoboehmite alumina. Then, a monovalent acid is added to the dispersion. The pH of the suspension is adjusted with a base to values ​​above 3, and the suspension is shaped by spray drying to form the microspherical catalyst particles.

[0037] The zeolites used preferably have a low sodium content (less than 1.5% by weight of Na2O) or are sodium-free. Suitable zeolites for use include zeolites such as Y zeolites, including HY, USY, dealuminized Y, RE-Y and RE-USY.

[0038] The term "boehmite" is used in industry to describe aluminum hydrates that exhibit X-ray diffraction (XRD) patterns similar to those of aluminum oxide-hydroxide [AlO(OH)]. In its synthetic form, it can have a crystalline structure called well-crystallized boehmite or microcrystalline boehmite, and pseudoboehmite, which is quasicrystalline boehmite. Microcrystalline boehmites have a smaller surface area, a high degree of crystallinity, a larger crystal size, and the X-ray peaks are of high intensity and narrower. Pseudoboehmite (quasicrystalline boehmite) has a larger surface area, a smaller crystal size, and wider, lower-intensity X-ray peaks, and disperses easily in water and acid.

[0039] The colloidal silica used in the synthetic matrix is ​​stabilized with ammonia and has a low sodium content. Kaolin is the clay normally used in the preparation of FCC catalysts as a synthetic matrix; other clays such as bentonite, saponite, sepiolite, attapulgite, laponite, hectorite, English clay, anionic clays such as hydrotalcite, or calcined kaolin transformed into meta-kaolin can also be used.

[0040] In the preparation of the catalyst for the present patent application, one or more Y zeolites were used, more specifically fausasitic type Y zeolites, modified by ion exchange with rare earths.

[0041] The catalytic compositions of the present invention (catalyst) have high contents of rare earth oxides (RE2O3), having a minimum content of at least 3% by weight based on the total weight of the catalyst and a maximum content of 5%. The metal oxide is present in the catalyst as an exchanged ion in the zeolite component. The rare earth metals include, but are not limited to, elements selected from the group consisting of lanthanide series elements, yttrium and their mixtures. Preferably, the rare earth metal is selected from the group consisting of lanthanum (La), praseodymium (Pr), neodymium (Nd) and cerium (Ce). Lanthanum (La) and cerium (Ce) are preferably used, with lanthanum (La) being even more preferred.

[0042] The catalytic compositions of the present invention, in addition to their high rare earth content, possess a pore system comprising pores in the micropore and mesopore range. Typically, the useful catalytic compositions of the present invention comprise a high matrix surface area to zeolite surface area (M / Z) ratio. For the purposes of the invention, the term "mesopore surface area" is used herein to indicate the surface area attributable to the catalytically active matrix, the material of which will have a pore size between 20 and 600 Angstroms as measured by the BET chart. Analogously, the term "micropore surface area" is used herein to indicate the surface area attributable to the catalytically active zeolite, the zeolite of which will have a pore size smaller than 20 Angstroms as measured by the BET chart. According to the present invention, the catalyst composition comprises an M / Z ratio of at least 1 up to 2.5.

[0043] The catalytic composition of the present invention can be used in any fluidized bed catalytic cracking process unit using 100% pure vegetable oil or lipid base as the feed stream. The 100% pure vegetable oil or lipid base feed stream must contain glycerides with fatty acids with carbon chains containing 9 to 20 carbon atoms (C9-C20) derived from animal or vegetable biomass, with concentrations greater than 50% by mass of fatty acids.

[0044] More specifically, vegetable oils such as soybean oil, macauba oil, castor oil (Ricinus communis), cottonseed oil (Gossypium hirsutum or G. barbadensis), palm oil (Elaeis guineensis), pine oil (Tall oil), sunflower oil (Helianthus annuus), jatropha oil (Jatropha curcas), and rapeseed oil, algae oil, or even animal fats such as beef tallow may be used as raw materials, comprising at least 15% by mass in relation to the total load processed in the FCC unit. The load stream may also contain a single oil or a mixture of two or more oils, in any proportions. Examples and test results of the invention

[0045] Combined catalyst compositions were tested under specific process conditions at the FCC. For the study of the present invention, the following tests were carried out, which represent examples of embodiments of the present invention, showing the results of processing vegetable oil or animal fat streams containing linear side chains with 9 to 20 carbon atoms for the production of aromatics.

[0046] The catalyst as described significantly increases the production of highly stable gasoline in the catalytic cracking process, as can be demonstrated by the examples shown here. EXAMPLE 1: Feedstock:

[0047] Soybean oil, containing approximately 18 carbon atoms, was used as feedstock, and its properties are shown in Table I. Table I - Characterization of soybean oil Catalyst:

[0048] In this example, two catalysts containing Y zeolite, catalysts C1 and C2, with two different levels of rare earth elements, were used. The characterization of the tested catalysts is shown in Table II. Test Units:

[0050] The FCC unit was tested in a demonstration unit operating with high feed rates of up to 200 kg / h. The unit's catalyst inventory is extremely high, around 300 kg. The unit has an adiabatic temperature control system for the main equipment: reactor riser, rectifier, and regenerator, which allows for studies involving the energy aspects of the process. Analyses:

[0051] The following yield groups were defined: fuel gas (hydrogen, methane, ethane, and ethene), LPG (C3 and C4 hydrocarbons, except propene), propene, gasoline (C5-220°C), LCO (220-343°C), decanted oil (DO: +343°C), coke, carbon monoxide, carbon dioxide, and water.

[0052] Coke yield was calculated from the mass flow rate of the combustion gas and its chromatographic composition.In general, studies in the literature calculate the water produced by the difference between 100% by weight and the sum of the other yields, or simply do not report how the water yield calculation was performed. In this example, the water yield was estimated by the total water calculated at the end of each experiment subtracted from the value fed into the unit (lifting, dispersion, rectification, and separation devices).

[0053] Samples of the total liquid effluent were collected for simulated distillation (ASTM D2887).

[0054] For a detailed characterization of the gasoline fraction, the liquid product was also subjected to the PIANO method, which provides the distribution of hydrocarbons (n-paraffins, i-paraffins, aromatics, naphthenes, olefins) with a boiling point of up to 220°C. The MON (Motor Octane Number) and RON (Research Octane Number) octane ratings were also calculated from gas chromatography. The sulfur content in the gasoline was measured.The gasoline distillation curve (ASTM D86) was also obtained.

[0055] The oxidation stability of gasoline was evaluated by the PetroOxy method and by the amount of current, washed and unwashed gum. In addition, the diene index and total oxygen content were analyzed in the gasoline distillation range. Experimental result:

[0056] In the experiment with the prior art catalyst C1, a faujasite zeolite-based catalyst with a moderate rare earth content was used. In the experiment with the catalyst of the present invention C2, a catalyst with a very high rare earth content (greater than 3%) was used, aiming at the conversion of oxygenated compounds into products, conversion of conjugated dienes and maximization of gasoline.

[0057] The feed temperature and reaction temperature were maintained at 190°C and 480°C, respectively, in all tests, with a feed flow rate of 150 kg / h and a catalyst circulation rate of 1350 kg / h, i.e., a catalyst / oil ratio of 9.0.The absolute pressure in the riser was maintained at 258 kPa, while the contact time in the riser was around 2.0 s. The rectification temperature was approximately 30°C lower than the reaction temperature in all tests. High conversions were achieved in both cases, around 77% by weight.

[0058] The results in Table III show the product yields and mass concentrations of saturates, olefins, and aromatics of interest calculated from the PIANO method (gas chromatography) in the gasoline range. Table III - Operating conditions, yields (% by weight relative to feed charge) and quality of naphtha produced.

[0059] The concentration of dienes is a good indication of naphtha stability and its potential for gum formation. The lower the diene concentration, the less gum formation and the greater the stability of the gasoline. The diene concentration is much lower when using the C2 catalyst with a higher rare earth content. The diene index obtained by high-performance liquid chromatography (HPLC) is very low, again indicating its high stability during transport, storage, and stockpiling.

[0060] The stability of gasoline during storage can also be measured by the induction period test, in which gasoline is subjected to an oxygen-rich atmosphere and must remain stable for at least 6 hours (360 min), where each hour represents 1 month of storage. Therefore, gasoline capable of remaining stable for 360 min of testing would withstand 6 months of storage.As a faster analytical alternative, the oxidation stability of gasoline was measured using the PetroOxy method, in which oxidation is accelerated, obtaining a result of 169 min for gasoline produced with C2. To obtain equivalence with the induction period, this value must be multiplied by 10, i.e., 1690 min, an extremely high value, exceeding the ANP specification.

[0061] Similarly, the washed gum method quantifies the presence of gum in gasoline. The maximum value specified by the National Petroleum Agency is 5.0 mg / 100 ml, while the value obtained in gasoline was lower than the detection limit of 0.5 mg / 100 ml for the C2 catalyst.

[0062] The C2 catalyst, with a higher rare earth content, not only converts the conjugated dienes of the product into more stable components in the gasoline produced, but also reduces the presence of oxygenated precursor compounds for gum formation in the product.The percentage of oxygen in gasoline with catalyst C2 was only 0.6% by mass, while with the conventional catalyst C1, the content reached 1.4% by mass. It is worth highlighting that the process described here results in gasoline superior to the state of the art, as it is 100% renewable and has exceptional stability, as can be seen from the excellent results in Table III: it has a maximum oxygen content of 0.6%, a washed gum content of less than 0.5 mg / 100 ml, a diene content of less than 0.25%, and oxygen oxidation stability by the PetroOxy method exceeding 40 minutes. Furthermore, its distillation range is typical of naphtha, between 34 and 204°C.

[0063] The high ratio between matrix surface area / catalyst zeolite surface area favors the initial conversion of high molecular weight glyceride molecules into lower molecular weight intermediates that will ultimately be converted by the rare earths present in the catalyst zeolite into stable compounds.

Claims

CLAIMS 1. A fluidized bed catalytic cracking process for glycerides to produce highly stable gasoline, characterized by contacting a feed stream of vegetable oils and / or animal fat containing glycerides with a catalyst based on ion-exchange modified faujasitic zeolite with rare earth oxides (RE2O3), wherein the catalyst contains at least 3% by weight of rare earth oxides relative to the total weight of the catalyst and a matrix surface area to zeolite surface area ratio (M / Z) of at least 1 under cracking conditions between 400°C and 520°C.

2. A process according to claim 1, characterized in that the feed stream of vegetable oils and / or animal fat contains glycerides with fatty acids with carbon chains containing 9 to 20 carbon atoms (C9 – C20) derived from vegetable and / or animal biomass. 3.A process according to claim 1, characterized by the feed stream containing glycerides with concentrations greater than 50% by mass of fatty acids.

4. A process according to claim 1, characterized by the vegetable oil being selected from soybean oil, macauba oil, castor oil (Ricinus communis), cottonseed oil (Gossypium hirsutum or G. barbadensis), palm oil (Elaeis guineensis), pine oil (Tall oil), sunflower oil (Helianthus annuus), jatropha curcas oil and rapeseed oil, and the animal fat being beef tallow.

5. A process according to claim 1, characterized by the feed stream containing... A single oil or a mixture of two or more oils, in any proportions.

6. Process according to claim 1, characterized in that the rare earth elements of the rare earth oxides (RE2O3) include elements selected from the group consisting of elements of the lanthanide series, yttrium and mixtures thereof.

7. Process according to claim 6, characterized in that the rare earth metal is selected from the group consisting of lanthanum (La), praseodymium (Pr), neodymium (Nd) and cerium (Ce).

8. Process according to claim 1, characterized in that the catalyst used is composed of several components: zeolites, active matrix (aluminas), synthetic matrix (silicas) and inert matrix (kaolin) in its chemical composition.

9. Process according to claim 8, characterized in that the matrix is ​​selected from the group consisting of silica, alumina and mixtures thereof. 10.

10. Process according to claim 1, characterized in that the contact time between the reactants and the catalyst is between 1.5 and 3.0 seconds in the riser reactor.

11. Process according to claim 1, characterized in that the catalyst / vegetable oil or animal fat ratio is between 3.0 and 20.0 in the riser reactor.

12. Process according to claim 1, characterized in that the absolute operating pressure in the riser reactor is between 200 and 400 kPa.

13. Gasoline with high stability characterized in that it is obtained by the process as defined in claim 1 and is 100% renewable, having a maximum content of 0.6% of...

13. Gasoline, characterized by having a distillation range between 34°C and 202°C. It is characterized by having a current washed gum content of less than 0.5 mg / 100 ml, a diene content of less than 0.25%, and oxygen oxidation stability greater than 40 minutes.

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