PURIFICATION OF RECYCLED AND RENEWABLE ORGANIC MATERIAL

Abstract

A method is provided herein for purifying a recycled or renewable organic material (10), wherein the recycled or renewable organic material (10) comprises more than 1 ppm of silicon as silicon compounds and / or more than 10 ppm of phosphorus as phosphorus compounds, comprising the steps of (a) providing a feed of the lipid material; (b) optionally pretreating (20) the recycled or renewable organic material (10) at 180 to 325°C and optionally adding acid before or after the heat treatment process and optionally filtering the thermally pretreated recycled or renewable organic material; (c) thermally treating (40) the recycled or renewable organic material (10) in the presence of an adsorbent at a temperature of 180 to 325°C and filtering (50) the thermally treated recycled or renewable organic material, and optionally adding acid before or after the heat treatment process;(d) optionally mixing the heat-treated recycled or renewable organic material with a hydrocarbon- or lipid-based stream; (e) optionally evaporating (30) the volatile silicon compounds from the heat-treated recycled or renewable organic material; and (f) hydrotreating (60) the lipid material in the presence of a hydrotreating catalyst; to obtain purified hydrotreated recycled or renewable organic material (61) comprising less than 20%, preferably less than 10%, more preferably less than 5%, of the original silicon content of the recycled or renewable organic material provided in step (a) and / or less than 30% of the original phosphorus content of the recycled or renewable organic material provided in step (a).

Description

Field of Invention The present invention relates to a method for purifying recycled or renewable organic material, in particular recycled or renewable organic material comprising 1 ppm of silicon as silicon compounds and / or more than 10 ppm of phosphorus as phosphorus compounds. Background of the Invention In some cases, recycled or renewable organic material contains high amounts of silicon (Si) as silicon compounds and high amounts of phosphorus as phosphorus compounds such as phospholipids. Before catalytic processing of recycled or renewable organic material, these impurities must be removed, as these compounds are known catalytic poisons and must therefore be eliminated before hydrotreating to maximize cycle time and the benefits of the hydrotreator. In particular, resin oil pitch (TOP) contains silicon and phosphorus impurities, which most likely originate from antifouling agents used in upstream processing. These antifouling agents include, for example, polydimethylsiloxanes (PDMS), which are oil-soluble, and Ref. 314422, therefore, difficult to remove from the oil. In addition, some other impurities may come from sand or dirt during wood collection. Removal of silicon impurities is required before hydrotreatment to avoid a reduced catalyst life in the unit. Conventional purification methods, such as filtration or bleaching, are not suitable for effectively removing silicon impurities. Brief Description of the Invention Therefore, an object of the present invention is to provide a method for overcoming the aforementioned problems. The objects of the invention are achieved by a method characterized by what is stated in the independent claims. Preferred embodiments of the invention are described in the dependent claims. The invention is based on the surprising discovery that recycled or renewable organic material containing high amounts of phosphorus and silicon compounds can be purified by a method that leads to the removal of phosphorus and silicon compounds from the recycled or renewable organic material. The organic material is subjected to a thermal treatment of the lipid feed material in the presence of an adsorbent at 180 to 325°C, and the lipid material is hydrotreated in the presence of a catalyst at a temperature of 270 to 380°C under a pressure of 4 to 20 MPa and under a continuous flow of hydrogen. The method allows the use of low-quality recycled or renewable organic raw materials as feedstock in hydrotreating, for example, in processes that produce high-quality renewable fuels and / or chemicals. Brief Description of the Figures The invention will now be described in greater detail by means of preferred embodiments with reference to the accompanying figures, in which Figure 1 illustrates a first exemplary process flow of the present method. Figure 2 illustrates the effect of acid treatment on the removal of Si and P from crude TOP samples. Figure 3 illustrates the effect of heat treatment on the removal of Si and P from crude TOP samples. Detailed Description of the Invention The present invention provides a method for purifying a recycled or renewable organic material. The term recycled or renewable organic material refers to organic material, that is, material containing carbon, obtained 1) from a natural resource that is replenished to overcome the depletion of the resource caused by its use and consumption, or 2) from a raw or processed material that is recovered from a residue for reuse. Recycled or renewable organic material characteristically comprises aliphatic compounds having a carbon chain of 4 to 30 carbon atoms, particularly 12 to 22 carbon atoms. Typical examples of such aliphatic compounds are fatty acids or their esters, particularly those where the fatty acids have an aliphatic chain of 4 to 30 carbon atoms, more specifically 12 to 22 carbon atoms. Recycled or renewable organic material typically comprises at least 50% by weight of aliphatic compounds of the total weight of the recycled or renewable organic material. Typically, recycled or renewable organic material refers to fats and / or oils of vegetable, microbial, algal, and / or animal origin. It also refers to any waste stream received from the processing of such oils and / or fats. Recycled or renewable organic material may be in unprocessed form (e.g., animal fat) or in processed form (used cooking oil). Vegetable fats and / or oils can come directly from plants or can be byproducts of various industrial sectors such as agriculture or forestry. For example, bio-oils and bio-crudes can be produced from biomass, also known as lignocellulosic biomass, using various liquefaction methods such as rapid pyrolysis or hydrothermal liquefaction. Rapid pyrolysis is the thermochemical decomposition of biomass through rapid heating in the absence of oxygen. Hydrothermal liquefaction (HTL) is a thermal depolymerization process used to convert wet biomass into crude oil at moderate temperatures and high pressures.Examples of bio-oil and bio-crude produced from lignocellulosic biomass, such as forestry harvest residues or sawmill byproducts, include lignocellulose pyrolysis liquid (LPL), produced by rapid pyrolysis, and HTL-bio-crude, produced by hydrothermal liquefaction. Another example of vegetable oil is resin oil, obtained as a byproduct of the Kraft wood pulp manufacturing process as crude resin oil (CTO) and its derivatives, such as resin oil pitch (TOP), crude fatty acids (CEA), resin oil fatty acids (TOFA), and distilled resin oil (DTO). Resin oil contains resin acids, fatty acids, and unsaponifiables. Resin acids are a mixture of organic acids derived from oxidation and polymerization reactions of terpenes.The main resin acid in resin oil is abietic acid, but abietic derivatives and other acids such as primaric acid are also present. Fatty acids are long-chain monocarboxylic acids found in hardwoods and softwoods. The main fatty acids in resin oil are oleic, linoleic, and palmitic acids. Unsaponifiables cannot be converted into soaps because they are neutral compounds that do not react with sodium hydroxide to form salts. They include sterols, higher alcohols, and hydrocarbons. Sterols are derivatives of spheroids that also contain a hydroxyl group. The term resin oil pitch (TOP) refers to the residual bottom fraction from the residue of resin oil distillation processes. Resin oil pitch typically comprises 34 to 51 wt% of free acids, 23 to 37 wt% of esterified acids, and 25 to 34 wt% of neutral unsaponifiable compounds of the total weight of resin oil pitch. The free acids are typically selected from a group consisting of dehydroabietic acid, abietic acid, and other resin acids. The esterified acids are typically selected from a group consisting of oleic and linoleic acids. The neutral unsaponifiable compounds are typically selected from a group consisting of diterpene sterols, fatty alcohols, sterols, and dehydrated sterols. The term crude fatty acid (CFA) refers to materials containing fatty acids that can be obtained by purification (e.g., distillation at reduced pressure, extraction and / or crystallization) from CTO. The term total oil fatty acid (TOFA) refers to the fatty acid-rich fraction from the distillation of crude oil (CTO). TOFA typically comprises primarily fatty acids, typically at least 80% by weight of the total TOFA weight. It typically contains less than 10% by weight of rosin acids. The term distilled resin oil (DTO) refers to the resin acid-rich fraction from the distillation of crude resin oil (CTO). DTO typically comprises primarily fatty acids, typically 55 to 90% by weight, and rosin acids, typically 10 to 40% by weight, of the total DTO weight. Typically, DTO comprises less than 10% by weight of neutral unsaponifiable compounds of the total distilled resin oil weight. The term microbial oils refers to triglycerides (lipids) produced by microbes. The term algal oils refers to oils derived directly from algae. The term animal fats and oils refers to lipid materials derived from animals. Examples of recycled or renewable organic material of the present invention include, but are not limited to, oils and fats of animal origin, oils and fats of vegetable or plant origin such as palm oil, used cooking oil, microbial oils, algae oils, free fatty acids, any lipid containing phosphorus and / or metals, oils from yeast or mold products, oils from biomass, rapeseed oil, canola oil, sunflower oil, soybean oil, hemp oil, olive oil, linseed oil, cottonseed oil, mustard oil, palm oil, peanut oil, castor oil, coconut oil, animal fats such as tallow, grease, recycled edible fats, raw materials produced by genetic engineering and biological raw materials produced by microbes such as algae and bacteria, resin oil, fatty acid from oil resin (TOFA),crude fatty acids (CFA), resin oil pitch (TOP) and any mixture of such raw materials. In particular, the recycled or renewable organic material is crude resin oil (CTO) or resin oil pitch (TOP). The recycled or renewable organic material to be treated with the current method contains high amounts of silicon compounds. The recycled or renewable organic material of the present invention comprises more than 1 ppm of silicon compounds. In particular, the recycled or renewable organic material of the present invention comprises more than 10 ppm of silicon compounds, more particularly the recycled or renewable organic material of the present invention comprises more than 15 ppm of silicon compounds, and even more particularly the recycled or renewable organic material of the present invention comprises more than 20 ppm of silicon compounds. The recycled or renewable organic material to be treated using the current method also contains high amounts of phosphorus compounds. The phosphorus compounds present in biomass-based lipid material are typically phospholipids. Specifically, the phospholipids present in biomass-based lipid material include one or more of the following: phosphatidylethanolamines, phosphatidylcholines, phosphatidylinositols, phosphatidic acids, and phosphatidylethanolamines. In particular, the recycled or renewable organic material of the present invention comprises more than 10 ppm, especially more than 20 ppm, particularly more than 50 ppm of phosphorus. The recycled or renewable organic material to be treated using this method may also include other impurities, such as phosphorus and / or metals in the form of phospholipids, soaps, and / or salts. These impurities may be, for example, in the form of phosphates or sulfates, iron salts or organic salts, soaps, or phospholipids. / ζ^ηηη / ίζηζ / Β / γίΛΐ Metallic impurities that may be present in biomass-based lipid material are, for example, alkali metals or alkaline earth metals, such as sodium or potassium salts, or magnesium or calcium salts, or any compound of such metals. Accordingly, a method for purifying a recycled or renewable organic material is provided herein, wherein the recycled or renewable organic material comprises more than 1 ppm of silicon as silicon compounds and / or more than 10 ppm of phosphorus as phosphorus compounds, comprising the steps of (a) providing a feed of recycled or renewable organic material; (b) optionally pretreating the recycled or renewable organic material thermally at 180 to 325°C and optionally adding acid before or after the thermal treatment process and optionally filtering the thermally pretreated recycled or renewable organic material; (c) heat treat the recycled or renewable organic material in the presence of an adsorbent at a temperature of 180 to 325°C and filter the heat-treated recycled or renewable organic material, and optionally add acid before or after the heat treatment process; (d) optionally mix the heat-treated recycled or renewable organic material with a hydrocarbon- or lipid-based stream; (e) optionally evaporating volatile silicon compounds from the heat-treated recycled or renewable organic material; and (f) hydrotreating the heat-treated recycled or renewable organic material in the presence of a hydrotreating catalyst; to obtain purified hydrotreated recycled or renewable organic material comprising less than 20%, preferably less than 10%, more preferably less than 5%, of the original silicon content of the recycled or renewable organic material provided in step (a) and / or less than 30% of the original phosphorus content of the recycled or renewable organic material provided in step (a). In step (c) the recycled or renewable organic material is heated to any temperature from 180 to 325°C. For optimal results, step (c) is carried out at between 200 and 300°C, preferably between 240 and 280°C. The time during which the recycled or renewable organic material is heated and held at the desired temperature, i.e., the residence time, is typically 1 to 300 min, preferably 5 to 240 min, more preferably 30 to 90 min in step (c). The pressure in step (c) is typically 500 to 5000 kPa, preferably 800 to 2000 kPa. / ζ^ηηη / ίζηζ / Β / γίΛΐ In step (c) the recycled or renewable organic material is heated to cause thermal reactions that alter the structure of the impurity-containing compounds included in the recycled or renewable organic material, thus forming material that is adsorbed onto the adsorbent present in the heating step (o), or material that forms solid precipitates and can therefore be subsequently removed from the recycled or renewable organic material. The adsorbent in step (c) may be selected from silica-based adsorbents. Preferably, the adsorbent is selected from a group consisting of aluminum silicate, silica gel, and mixtures thereof. In step (o), the amount of adsorbent is typically 0.1 to 10.0% by weight, preferably 0.5 to 2.0% by weight, of the total weight of the treated recycled or renewable organic material. The process can be further improved by adding acid before or after the heat treatment in step (c). This removes any remaining sodium impurities. The acid is preferably selected from citric acid and phosphoric acid. After heat treatment, the adsorbent, which contains unwanted impurities, is removed. Therefore, in step (c), the recycled or renewable organic material undergoes removal of the solid adsorbent material. This removal can be achieved, for example, by any separation method deemed suitable by a person skilled in the art for separating the solid material from the heat-treated recycled or renewable organic material. Suitable examples include, but are not limited to, filtration, centrifugation, and phase separation. It should also be understood that several separation methods, such as filtration and centrifugation, can be combined. The removal is preferably carried out at a temperature between 100 and 180°C. Before step (c), the recycled or renewable organic material may undergo thermal pretreatment in the absence of adsorbent material. In the optional step (b), the recycled or renewable organic material is preheated to induce thermal reactions that disrupt silicon-containing impurities within the material, creating volatile silicon compounds that can be subsequently removed. In particular, polydimethylsiloxanes (PDMS) resulting from antifouling agents are degraded to volatile polydimethylcyclosiloxanes (PDMCS) under the process conditions. The heat pretreatment of step (b) takes place at any temperature from 180 to 325°C. To achieve optimal results, step (b) is carried out from 200 to 300°C, preferably from 240 to 280°C. The time during which the recycled or renewable organic material is heated and held at the desired temperature, i.e., the residence time, is typically 1 to 300 min, preferably 5 to 90 min, more preferably 20 to 40 min in step (b). The pressure in the heat pretreatment in step (b) is typically 500 to 5000 kPa, preferably 800 to 2000 kPa. Optionally, the process can be further improved by adding acid before or after the heat pretreatment in step (b). This removes any remaining sodium impurities. The acid is preferably selected from citric acid and phosphoric acid. In step (b), the solid material created due to the heat treatment can be removed. The removal of the solid material can be achieved, for example, by any separation method that an expert considers suitable for separating the solid material from the heat-treated recycled or renewable organic material. Suitable examples include, but are not limited to, filtration, centrifugation, and phase separation. It should also be understood that several separation methods, for example, filtration and centrifugation, can be combined. Preferably, the removal is carried out by filtration. The removal is preferably carried out at any temperature between 100 and 180°C. The removal of solids / precipitates prevents the deactivation of the hydrotreating catalyst in the hydrotreating of recycled or renewable organic material. After the heat treatment in step (c), volatiles created due to the heat treatment and / or present in the recycled or renewable organic material can be removed. Therefore, in step (e), the heat-treated recycled or renewable organic material is optionally subjected to evaporation of the volatile silicon compounds in one or more stages. In step (e), evaporation is achieved at any temperature between 145 and 250°C, particularly between 150°C and 225°C. For optimal results, evaporation in step (e) is carried out between 160°C and 200°C, preferably between 160°C and 180°C. The reduced pressure in the evaporation step (e) is such that the evaporation of volatile Si compounds is achieved. Typically, the pressure is 0.1 to 5 kPa, preferably 0.1 to 3 kPa. The evaporated mass must be disposed of appropriately for an evaporation of 1 to 10% by weight, preferably 1 to 8% by weight, more preferably 1 to 5% by weight, even more preferably 1 to 3% by weight, of the thermally treated recycled or renewable organic material. The time during which the heat-treated recycled or renewable organic material is heated and evaporated to the desired temperature, i.e., the residence time, is typically 100 to 600 min, preferably 180 to 300 min in the evaporation phase of step (e). An applicable step (e) provides (i) a vapor fraction comprising most of the volatile silicon compounds, and (ii) a heat-treated recycled or renewable organic material fraction comprising less than 50%, preferably less than 30%, of the original silicon content of the recycled or renewable organic material provided in step (a). Evaporation in step (e) can be achieved by any evaporation method that an expert considers suitable for separating volatiles from the heat-treated recycled or renewable organic material. Suitable examples include, but are not limited to, falling-film evaporation, rising-film evaporation, thin-film evaporation, and flash evaporation. Evaporation can be carried out in one or more stages. It should also be understood that several evaporation methods, such as thin-film evaporation and flash evaporation, can be combined. / ζ^ηηη / ίζηζ / Β / γίΛΐ The preferred evaporation method of the present invention is flash evaporation in one or more stages. Due to the high pressure differential in the flash evaporation vessel, less mass of material is required in flash evaporation to provide better mass transfer compared to thin-film evaporation. For example, applying the same method and equipment as in a typical thin-film evaporation process from crude resin oil (CTO) to resin oil pitch (TOP) after heat treatment significantly increases heat consumption compared to flash evaporation. The optimal temperature, pressure, evaporated mass, and number of evaporation stages to use depend on the composition and quality of the recycled or renewable organic material and also on the heat treatment parameters (temperature, pressure, and residence time) of step (c) and optional steps (b) and (e). Furthermore, it is preferable to add water to the initial mixture of the heat-treated recycled or renewable organic material. Adding a small percentage of water to the initial heat-treated recycled or renewable organic material allows the use of a lower temperature and higher vacuum pressure while achieving the same level of Si removal as in normal evaporation. Even more importantly, there is less loss of volatile fatty acids, reducing the amount of fatty acid residue by half compared to evaporation without water. Accordingly, in an example of the present invention, water is added to the heat-treated recycled or renewable organic material so that the water content before the evaporation step (e) is 1 to 5% by weight, preferably 1.5 to 4% by weight, more preferably 2 to 3% by weight of the total weight of the heat-treated recycled or renewable organic material. The purified recycled or renewable organic material is subjected to (f) hydrotreatment in the presence of a hydrotreatment catalyst to further remove silicon from the recycled or renewable organic material. The heat-treated recycled or renewable organic material may (d) be blended with a hydrocarbon- or lipid-based stream if desired. The hydrocarbon- or lipid-based stream is preferably vacuum gas oil (VGO). The term hydrotreating refers to a chemical engineering process in which the reaction of hydrogen is used to remove impurities, such as oxygen, sulfur, nitrogen, phosphorus, silicon, and metals, especially as part of oil refining. Hydrotreating can be carried out in one or several steps in one or more reactor units or catalyst beds. Step (f) is typically achieved under continuous hydrogen flow. For optimal results, the continuous hydrogen flow in step (f) preferably has an H2 / feed ratio of 500 to 2000 nL / L, more preferably 800 to 1400 nL / L. In step (f), the hydrotreating is carried out appropriately at a temperature of 270 to 380°C, preferably 275 to 360°C, more preferably 300 to 350°C. Normally, the pressure in step (f) is 4 to 20 MPa. The hydrotreating catalyst in step (f) preferably comprises at least one component selected from IUPAC group 6, 8 or 10 of the periodic table. Preferably, the hydrotreating catalyst in step (f) is a supported Pd, Pt, Ni, NiW, NiMo or CoMo catalyst and the support is zeolite, zeolite-alumina, alumina and / or silica, preferably N1W / Al2O3, NiMO / Al2O3 or CoMO / Al2O3. In particular, the hydrotreating catalyst is a sulfide NiW, NiMO or CoMo catalyst. The time during which the recycled or renewable organic material is heated and held at the desired temperature, i.e., the residence time, is typically 1 to 300 min, preferably 5 to 240 min, more preferably 30 to 90 min in step (c). An applicable hydrotreating step (f) provides a purified and hydrotreated recycled or renewable organic material. The purified hydrotreated recycled or renewable organic material appropriately comprises less than 20%, more preferably less than 10%, and even more preferably less than 5%, of the original silicon content of the recycled or renewable organic material provided in step (a) and / or less than 30% of the original phosphorus content of the recycled or renewable organic material provided in step (a). To achieve optimal results, some of the hydrogen-treated recycled or renewable organic material may be recycled in step (f). Preferably, the ratio of fresh feed, i.e., purified recycled or renewable organic material obtained in step (c), to recycled hydrotreated recycled or renewable organic material is 2:1 to 20:1. In one particular example, step (f) is achieved by (fl) hydrodeoxygenation (HDO) of the heat-treated recycled or renewable organic material fraction. This is preferably achieved in the presence of an HDO catalyst at a temperature of 290 to 350°C under a pressure of 4 to 20 MPa and under a continuous flow of hydrogen. The term hydrodeoxygenation (HDO) refers to / ζ^ηηη / ίζηζ / Β / γίΛΐ the removal of oxygen as water by means of molecular hydrogen under the influence of a catalyst (HDO). The HDO catalyst can be selected, for example, from a group consisting of NiMO catalysts, such as NiW and any mixture thereof. Preferably, the HDO catalyst is a sulfide NiW, NiMo, or CoMo catalyst. Suitablely, the continuous flow of hydrogen has an H2 / feed ratio of 500 to 2000 nL / L, preferably 800 to 1400 nL / L. Preferably, step (fl) is carried out to obtain purified recycled or renewable organic material comprising less than 1% by weight of oxygen. In another example, step (f) is achieved by (f2) hydrodesulfurization (HSD) of the thermally treated recycled or renewable organic material fraction. The term hydrodesulfurization (HDS) refers to the removal of sulfur as hydrogen sulfide by means of molecular hydrogen under the influence of a catalyst (HDS). In another example, step (f) is achieved by (f3) hydrometallization (HDM) of the heat-treated recycled or renewable organic material fraction. The term hydrodemetallization (HDM) refers to the removal of metals by trapping them with a catalyst (HDM). In another example, step (f) is achieved by (f4) hydrodenitrification (HDN) of the thermally treated recycled or renewable organic material fraction. The term hydrodenitrification (HDN) refers to the removal of nitrogen by means of molecular hydrogen under the influence of a catalyst (HDN). In another example, step (f) is achieved by (f5) hydrodesaromatization (HDA) of the heat-treated recycled or renewable organic material fraction. The term hydrodesaromatization (HDA) refers to the saturation or ring opening of aromatics by molecular hydrogen under the influence of an HDA catalyst. Figure 1 illustrates a first exemplary process flow of the present method. With reference to Figure 1, a feed of recycled or renewable organic material, in particular resin oil pitch (TOP) 10, is subjected to a heat treatment step 20 of the recycled or renewable organic material as described herein for step (b). The heat-treated feed of recycled or renewable organic material can then be evaporated 30 as described herein for step (e), and a bottoms containing a fraction 31 of heat-treated recycled or renewable organic material comprising less than 50% of the original silicon content of the recycled or renewable organic material provided in step (a), and a vapor fraction 32 comprising most of the volatile silicon compounds is obtained.The heat-treated recycled organic material 31 is then heated 40 in the presence of an adsorbent to adsorb the impurities to the adsorbent and make the mixture separable as described herein for step (c). The adsorbent is then separated 50 from the treated feed of recycled or renewable organic material as described herein for step (c) to obtain a purified recycled or renewable organic material 51 and an adsorbent 52 comprising most of the impurities.The purified recycled or renewable organic material is then hydrotreated 60, as discussed herein for step (f), to obtain a purified hydrogen-treated recycled or renewable organic material 61, wherein the purified hydrotreated recycled or renewable organic material comprises less than 20%, preferably less than 10%, and more preferably less than 5%, of the original silicon content of the recycled or renewable organic material provided in step (a) and / or less than 30% of the original phosphorus content of the recycled or renewable organic material provided in step (a). The hydrogen-treated recycled or renewable organic material 61 may then be subjected to catalytic enhancement 70. / zfrnnn / Lznz / E / YiAi After the recycled or renewable organic material has been purified according to the present method, it may undergo further processing, such as catalytic enhancement. Such catalytic enhancement processes include, but are not limited to, catalytic cracking, catalytic hydrocracking, thermocatalytic cracking, catalytic hydrotreating, fluid catalytic cracking, catalytic ketoning, and catalytic esterification. These processes require that the recycled or renewable organic material be sufficiently pure and free from impurities that could otherwise hinder the catalytic process or poison the catalyst(s) present in the process. Accordingly, the present invention further provides a process for producing recycled or renewable hydrocarbons, comprising the steps of (x) purifying the recycled or renewable organic material as described herein, and (y) subjecting the purified recycled or renewable organic material to a petroleum refinery conversion process, wherein the petroleum refinery conversion process comprises altering the molecular weight of the feed, such as hydrocracking or steam cracking, removing heteroatoms from the feed, such as thermal catalytic cracking, fluid catalytic cracking, or hydrotreating, in particular hydrodeoxygenation, hydrodesulfurization, altering the degree of saturation of the feed, such as hydrotreating, thermal catalytic cracking, or fluid catalytic cracking, and rearranging the molecular structure of the feed, such as isomerization.or any combination thereof to obtain at least one recycled or renewable hydrocarbon. In a typical example of the present process, the recycled or renewable hydrocarbon is a renewable traffic fuel or fuel component. In an example of the present process, step (y) is hydrocracking. In such an example, step (y) is preferably carried out in a mild hydrocracking (MHC) refinery unit, particularly in the presence of a hydrocracking catalyst. In another example of the present process, step (y) is steam cracking. In such an example, step (y) is preferably carried out in a steam cracking unit. In another example of the present process, step (y) is isomerization. In such an example, step (y) is preferably carried out in an isomerization unit. In another example of the present process, step (y) is hydrotreating. In such an example, step (y) is preferably carried out in a hydrotreating unit. In another example of the present process, step (y) is thermal catalytic cracking (TCC). In such an example, step (y) is preferably carried out in a thermal catalytic cracking unit. In another example of the present process, step (y) is fluid catalytic cracking (FCC). In such an example, step (y) is preferably carried out in a fluid catalytic cracking unit. EXPERIMENTAL Example 1 Crude TOP was treated in the presence of two adsorbents: aluminum silicate (Tonsil 9194 FF) and silica gel (Trisyl). The amount of each adsorbent was 1.5% by weight. Samples of crude TOP from different producers were tested. A 0.4% by weight addition of water was carried out before the high-temperature adsorption treatment. During the high-temperature adsorption treatment, the sample materials were heated to 280°C for 60 minutes. After this treatment, the sample materials were cooled to 100°C and filtered through 0.45 µm filter paper. Based on the results obtained, it can be seen that Si and other impurities can be very effectively removed from the feed at elevated temperatures in the presence of alumina silicate and silica gel adsorbent. However, more efficient purification was achieved using silica gel material. The results are listed in Table 1. / zfrnnn / Lznz / E / YiAi As can be seen in Table 2 and Figure 2 and Figure 3, the effective removal of Si and P cannot be achieved by simple acid + heat treatment or by an acid adsorption purification method. Table 1. Effect of adsorption by heat treatment on the removal of Si and P from different types of crude TOP samples. Addition of adsorbent at 1.5 wt% / zfrnnn / Lznz / E / YiAi 14144865 14225369 14225368 TOP crude A 280°C, 1 hour 280°C, 1 hour 1.5% by weight of Tonsil 9194 1.5% by weight of Trisyl Al mg / kg 7.1 3.7 <0.2 Fe mg / kg 27 32 2.4 Na mg / kg 580 150 150 Si mg / kg 27 3 1.3 Ca mg / kg 56 13 0.82 Mg mg / kg 6.2 14 <0.3 P mg / kg 50 14 <0.6 14177357 14225371 14225370 TOP crude B 280°C, 1 hour 280°C 1.5% by weight of Trisyl 1.5% in Tonsil weight 9194 Al mg / kg 10 4 <0.2 Fe mg / kg 71 50 0.62 Na mg / kg 740 180 170 Si mg / kg 130 12 4.4 Ca mg / kg 41 13 0.57 Mg mg / kg 7.4 13 <0.3 P mg / kg 137 21 1.3 Table 2. Effect of acid treatment (addition of 2000 ppm citric acid) and adsorption on the removal of Si and P from the crude TOP sample. Adsorbent added at 2.0 wt%. / zfrnnn / Lznz / E / YiAi 14151662 14151646 TOP crude C Bleaching at 120°C + cake filtration 2% by weight of Tonsil 9194 Al mg / kg 5 0.64 Fe mg / kg 29 1.1 Na mg / kg 490 6.9 Si mg / kg 41 15 Ca mg / kg 25 4.5 Mg mg / kg 4.2 1.5 P mg / kg 73 9.5 It will be obvious to a person skilled in the art that, as technology advances, the inventive concept can be implemented in various ways. The invention and its embodiments are not limited to the examples described above but may vary within the scope of the claims. It is hereby stated that, as of this date, the best method known to the applicant for putting the present invention into practice is the one that is clear from the present description of the invention.

Claims

1. A method for purifying a recycled or renewable organic material, wherein the recycled or renewable organic material comprises more than 1 ppm of silicon as silicon compounds and / or more than 10 ppm of phosphorus as phosphorus compounds, characterized in that it comprises the steps of (a) providing a feed of the recycled or renewable organic material, wherein the recycled or renewable organic material is selected from a group consisting of vegetable fats and oils, animal fats and oils, fossil waste oils, waste oil, algae oils, and microbial oils; (b) optionally thermally pretreating the recycled or renewable organic material at 180 to 325°C and optionally adding acid before or after the heat treatment process and optionally filtering the thermally pretreated recycled or renewable organic material;(c) heat-treating the recycled or renewable organic material in the presence of an adsorbent selected from silica-based adsorbents at a temperature of 180 to 325°C and filtering the heat-treated recycled or renewable organic material, and optionally adding acid before or after the heat treatment process; (d) optionally mixing the heat-treated recycled or renewable organic material with a hydrocarbon- or lipid-based stream; (e) optionally evaporating volatile silicon compounds from the heat-treated recycled or renewable organic material; and (f) hydrotreating the heat-treated recycled or renewable organic material in the presence of a hydrotreating catalyst;to obtain purified hydrotreated renewable or recycled organic material comprising less than 20%, preferably less than 10%, more preferably less than 5%, of the original silicon content of the recycled or renewable organic material provided in step (a) and / or less than 30% of the original phosphorus content of the recycled or renewable organic material provided in step (a).; 2. The method according to claim 1, characterized in that the recycled or renewable organic material is (b) heat-treated at 180 to 325°C to form a heat-treated recycled or renewable organic material.

3. The method according to claim 2, characterized in that the heat treatment (20) in step (b) is carried out at a temperature of 200 to 300°C, preferably at a temperature of 240 to 280°C.

4. The method according to claim 2 or 3, characterized in that the residence time is from 1 to 300 min, preferably from 5 to 90 min, more preferably from 20 to 40 min in the heat treatment of step (b).

5. The method according to any of claims 2 to 4, characterized in that the evaporation in step (e) is carried out at 150°C to 225°C, preferably at 160°C to 200°C, more preferably at 160°C to 180°C.

6. The method according to any of claims 2 to 5, characterized in that the pressure in the evaporation of step (e) is from 0.1 to 5 kPa, preferably from 0.1 to 3 kPa.

7. The method according to any of claims 2 to 6, characterized in that in the evaporation of step (e) 1 to 10% by weight, preferably 1 to 8% by weight, more preferably 1 to 5% by weight, even more preferably 1 to 3% by weight, of the heat-treated recycled or renewable organic material is evaporated.

8. The method according to any of claims 2 to 7, characterized in that water is added to the heat-treated recycled or renewable organic material such that the water content of the heat-treated recycled or renewable organic material before the evaporation step (e) is 1 to 5% by weight, preferably 1.5 to 4% by weight, more preferably 2 to 3% by weight.

9. The method according to any of claims 1 to 8, characterized in that the temperature in step (c) is from 200 to 300°C, preferably from 240 to 280°C.

10. The method according to any of claims 1 to 9, characterized in that the residence time is from 1 to 300 min, preferably from 5 to 240 min, more preferably from 30 to 90 min in step (c).

11. The method according to any of claims 1 to 10, characterized in that the pressure in step (c) is from 500 to 5000 kPa, preferably from 800 to 2000 kPa.

12. The method according to any one of claims 1 to 11, characterized in that the silicate-based adsorbents are selected from a group consisting of alumina silicate, silica gel, and mixtures thereof.

13. The method according to any of claims 1 to 12, characterized in that the amount of adsorbent is from 0.1 to 10.0% by weight, preferably 0.5 to 2.0% by weight, of the total weight of the treated recycled or renewable organic material.

14. The method according to any of claims 1 to 13, characterized in that acid is added before or after the heat treatment in step (c). / ζ^ηηη / ίζηζ / Β / γίΛΐ 15. The method according to any of claims 1 to 14, characterized in that the hydrotreatment step (f) takes place under a continuous flow of hydrogen.

16. The method according to claim 15, characterized in that in step (f) the continuous flow of hydrogen has an H2 / feed ratio of 500 to 2000 nL / L, preferably 800 to 1400 nL / L.

17. The method according to any of claims 1 to 16, characterized in that step (f) is carried out at a temperature of 270 to 380°C, preferably 275 to 360°C, more preferably 300 to 350°C.

18. The method according to any of claims 1 to 17, characterized in that step (f) is carried out at a pressure of 4 to 20 MPa.

19. The method according to any of claims 1 to 18, characterized in that the hydrotreating catalyst in step (f) comprises at least one component selected from IUPAC group 6, 8 or 10 of the periodic table.

20. The method according to any of claims 1 to 19, characterized in that the hydrotreating catalyst in step (f) is a supported Pd, Pt, Ni, NiW, NiMo or CoMo catalyst and the support is zeolite, zeolite-alumina, alumina and / or silica, preferably NiW / Al2O3, NiMo / Al2O3 or CoMo / Al2O3.

21. The method according to any of claims 1 to 20, characterized in that step (f) is carried out by (fl) hydrodeoxygenation (HDO) of the thermally treated recycled or renewable organic material fraction.

22. The method according to claim 21, characterized in that step (f) is achieved by (fl) hydrodeoxygenation (HDO) of the thermally treated recycled or renewable organic material fraction in the presence of an HDO catalyst at a temperature of 290 to 350°C under a pressure of 4 to 20 MPa and under continuous flow of hydrogen to obtain purified recycled or renewable organic material comprising less than 20%, preferably less than 10%, more preferably less than 5%, of the original silicon content of the recycled or renewable organic material provided in step (a).

23. The method according to claim 22, characterized in that in step (fl) the HDO catalyst is a sulfurized NiW, NiMO or CoMo catalyst.

24. The method according to claim 22 or 23, characterized in that in step (fl) the continuous flow of hydrogen has an H2 / feed ratio of 500 to 2000 nL / L, preferably 800 to 1400 nL / L.

25. The method in accordance with any of claims 1 to 24, characterized in that a portion of the hydrotreated product is recycled in step (f).

26. The method according to claim 25, characterized in that the ratio of fresh feed to hydrotreated product is from 2:1 to 20:

1.

27. The method according to any of claims 1 to 26, characterized in that in step (d) the hydrocarbon or lipid-based stream is vacuum gas oil (VGO) or animal fat.

28. A process for producing recycled or renewable hydrocarbons, characterized in that it comprises the steps of (x) purifying the recycled or renewable organic material in accordance with any of claims 1 to 27, and (y) subjecting the purified recycled or renewable organic material to a petroleum refinery conversion process, wherein the petroleum refinery conversion process comprises altering the molecular weight of the feed, removing heteroatoms from the feed, altering the degree of saturation of the feed, rearranging the molecular structure of the feed, or any combination thereof to obtain at least one recycled or renewable hydrocarbon.

29. The process according to claim / ζ^ηηη / ίζηζ / Β / γίΛΐ 28, characterized in that step (y) is hydrocracking.

30. The process according to claim 29, characterized in that step (y) is carried out in a mild hydrocracking (MHC) refinery unit.

31. The process according to claim 29 or 30, characterized in that step (y) is carried out in the presence of a hydrocracking catalyst.

32. The process according to claim 28, characterized in that step (y) is steam cracking.

33. The process according to claim 28, characterized in that step (y) is isomerization.

34. The process according to claim 28, characterized in that step (y) is hydrotreating.

35. The process according to claim 28, characterized in that step (y) is thermal catalytic cracking.

36. The process according to claim 2 8, characterized in that step (y) is fluid catalytic cracking.