Refinement of recycled and renewable organic materials

Abstract

In the present invention, there is provided a method for purifying recycled or renewable organic material, wherein the recycled or renewable organic material contains one or more impurities selected from the group consisting of silicon compounds, phosphorus compounds, Cl, and sterols, and the method includes the steps of: (a) providing a recycled or renewable organic material; (b) optionally preheating the recycled or renewable organic material at 180-325°C, and optionally adding an acid before or after the preheating process, and optionally filtering the preheat-treated recycled or renewable organic material after the preheating treatment; (c) heat-treating the recycled or renewable organic material at a temperature of 100-450°C, optionally in the presence of an adsorbent, and optionally adding water before or during the heat treatment process, to obtain a purified, hydrotreated recycled or renewable organic material. (d) optionally evaporating volatile silicon compounds from the heat-treated recycled or renewable organic material compounds, thereby reducing the silicon content of the heat-treated recycled or renewable organic material; (e) optionally pyrolyzing the recycled or renewable organic material, thereby reducing the oxygen and phosphorus content of the heat-treated recycled or renewable organic material, and optionally removing volatiles from the pyrolyzed recycled or renewable organic material, and optionally removing solids / precipitates from the recycled or renewable organic material; and (f) hydrotreating the heat-treated recycled or renewable organic material in the presence of a hydrotreating catalyst.

Description

Technical Field

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[0001] The present invention relates to a method for purifying recycled or renewable organic materials, particularly recycled or renewable organic materials containing one or more impurities selected from the group consisting of silicon compounds, phosphorus compounds, chlorine compounds, and metals.

Background Art

[0002] Recycled or renewable organic materials may contain a large amount of silicon (Si) as a silicon compound and a large amount of phosphorus as a phosphorus compound such as a phospholipid. Before the catalytic treatment of recycled or renewable organic materials, these impurities need to be removed from the materials because these compounds are catalyst poisons and should therefore be removed before the hydrogenation treatment in order to maximize the cycle life and profit of the hydrogenation treatment apparatus.

Summary of the Invention

[0003] The object of the present invention is therefore to provide a method capable of overcoming the above problems. The object of the present invention is achieved by a method characterized by the matters described in the independent claims. Preferred embodiments of the present invention are described in the dependent claims.

[0004] The present invention is based on the surprising discovery that a recycled or renewable organic material containing a large amount of phosphorus compounds and silicon compounds can be purified by subjecting the recycled or renewable organic material to a step of heat-treating the recycled or renewable organic material at 100 to 450 ° C, a step of filtering the material, and a step of hydrogenating the heat-treated recycled or renewable organic material in the presence of a hydrogenation catalyst, leading to the removal of phosphorus compounds and silicon compounds from the recycled or renewable organic material.

[0005] In the following, the present invention will be described in more detail by preferred embodiments with reference to the accompanying drawings. [Brief explanation of the drawing]

[0006] [Figure 1] Figure 1 shows a first exemplary process flow of the method of the present invention. [Figure 2] Figure 2 shows a second exemplary process flow of the method of the present invention. [Figure 3] Figure 3 shows the effect of acid treatment on the removal of Si and P from a crude TOP sample. [Figure 4] Figure 4 shows the effect of heat treatment on the removal of Si and P from a crude TOP sample. [Modes for carrying out the invention]

[0007] This invention provides a method for purifying recycled or renewable organic materials.

[0008] The term “recycled or renewable organic material” means organic material, i.e., carbon-containing material, obtained either 1) from natural sources to replenish the depletion of sources caused by its use and consumption, or 2) from raw materials or processed materials for reuse recovered from waste. Recycled or renewable organic material is characteristically characterized by containing aliphatic compounds having carbon chains of 4 to 30 carbon atoms, preferably 12 to 22 carbon atoms. Typical examples of such aliphatic compounds include fatty acids or their esters, particularly those fatty acids having aliphatic chains of 4 to 30 carbon atoms, more particularly 12 to 22 carbon atoms. Recycled or renewable organic material typically contains at least 50 wt% aliphatic compounds by weight of the total weight of the recycled or renewable organic material.

[0009] Typically, recycled or renewable organic materials refer to fats and / or oils of plant, microorganism, seaweed, and / or animal origin. It also refers to any waste stream resulting from the processing of such oils and / or fats. Recycled or renewable organic materials can be in an unprocessed form (e.g., animal fat) or a processed form (used cooking oil). Recycled or renewable organic materials also refer to fossil waste-based oils or waste oils.

[0010] The term "plant-based fats and oils" means fats and / or oils of plant origin, i.e., oils that can be directly derived from plants, or by-products from various industrial sectors such as agriculture or forestry.

[0011] Examples of plant-based fats and oils of the present invention include, but are not limited to, palm oil sludge, rapeseed oil, canola oil, colza oil, sunflower oil, soybean oil, hemp seed oil, olive oil, linseed oil, cottonseed oil, mustard oil, palm oil, peanut oil, castor oil, and coconut oil.

[0012] Other examples of plant-based fats and oils include biocrudes and biooils. Biocrudes and biooils are produced from biomass, particularly lignocellulosic biomass, using various liquefaction methods, such as hydrothermal liquefaction, or by pyrolysis, particularly rapid pyrolysis.

[0013] The term "biocrude" refers to oil produced from biomass by hydrothermal liquefaction. The term "bio oil" refers to pyrolysis oil produced from biomass by thermal decomposition. The term "biomass" refers to materials derived from living organisms that were recently alive, including plants, animals, and their by-products. The term "lignocellulosic biomass" refers to biomass derived from plants or their by-products. Lignocellulosic biomass consists of carbohydrate polymers (cellulose, hemicellulose) and aromatic polymers (lignin).

[0014] The term "pyrolysis" refers to the thermal decomposition of a material at an elevated temperature in a non-oxidizing atmosphere. The term "fast pyrolysis" refers to the thermochemical decomposition of biomass through rapid heating in the absence of oxygen. The term "hydrothermal liquefaction" (HTL) refers to a thermal depolymerization process used to convert wet biomass into crude-like oil under appropriate temperature and pressure conditions.

[0015] Examples of bio-oils and biocrudes produced from lignocellulosic biomass, such as forest harvest residues or sawmill by-products, include lignocellulosic pyrolysis liquid (LPL) produced by rapid pyrolysis and HTL-biocrudes produced by hydrothermal liquefaction.

[0016] Further examples of plant-based fats and oils include crude tall oil (CTO) and its derivatives obtained as by-products of the kraft process (wood pulping), such as tall oil pitch (TOP), crude fatty acids (CFA), tall oil fatty acids (TOFA), and distilled tall oil (DTO).

[0017] Crude tall oil contains resin acids, fatty acids, and unsaponifiable matter. Resin acids are a mixture of organic acids obtained from the oxidation and polymerization reactions of terpenes. The main resin acid in crude tall oil is abietic acid, but abietic acid derivatives and other acids, such as pimaric acid, are also found. Fatty acids are long-chain monocarboxylic acids and are found in hardwoods and softwoods. The main fatty acids in crude tall oil are oleic acid, linoleic acid, and palmitic acid. Unsaponifiable matter is a neutral compound that does not react with sodium hydroxide to form salts and therefore cannot be converted into soap. These include sterols, higher alcohols, and hydrocarbons. Sterols are steroid derivatives that also contain hydroxyl groups.

[0018] The term "tall oil pitch (TOP)" refers to the bottom fraction of the residue from the crude tall oil (CTO) distillation process. Tall oil pitch typically contains 34–51 wt% free acids, 23–37 wt% esterified acids, and 25–34 wt% unsaponifiable neutral compounds, relative to the total weight of the tall oil pitch. The free acids are typically selected from the group consisting of dehydroabietic acid, abietin, and other resin acids. The esterified acids are typically selected from the group consisting of oleic acid and linoleic acid. The unsaponifiable neutral compounds are typically selected from the group consisting of diterpene sterols, fatty alcohols, sterols, and sterol dehydrates.

[0019] The term "crude fatty acid (CFA)" refers to fatty acid-containing material that can be obtained by the purification of CTO (e.g., distillation, extraction, and / or crystallization under reduced pressure).

[0020] The term "tall oil fatty acid (TOFA)" refers to the fatty acid-rich fraction from the crude tall oil (CTO) distillation process. TOFA typically contains fatty acids, usually at least 80 wt% of its total weight. Typically, TOFA contains less than 10 wt% rosin acid.

[0021] The term "distilled tall oil (DTO)" means the resin acid-rich fraction of the crude tall oil (CTO) distillation process. DTO typically contains fatty acids, typically 55 - 90 wt% based on the total weight of DTP, and rosin acids, typically 10 - 40 wt% based on the total weight of DTP. Typically, DTO contains less than 10 wt% of non-saponifiable neutral compounds based on the total weight of the distilled tall oil.

[0022] The term "animal based fats and oils" means fats and / or oils of animal origin, i.e., liquid materials of animal origin. Examples of animal based fats and oils include, but are not limited to, for example, suet, tallow, fat, lard, whale oil, milk fat, fish oil, poultry oil and poultry fat.

[0023] The term "microbial oils" means triglycerides (lipids) produced by microorganisms.

[0024] The term "algal oils" means oils directly derived from algae.

[0025] The term "fossil waste-based oils" means oils produced from waste streams such as waste plastics or waste tires. Examples of fossil waste-based oils include, for example, waste plastic pyrolysis oil (WPPO) and end-of-life tire pyrolysis oil (ELTPO).

[0026] The term "waste oils" means any oil that has become unsuitable for its original purpose through contamination, the presence of impurities or loss of its original properties. Examples of waste oils include used lubricating oil (ULO), hydraulic oil, transformer oil or oil used in metalworking.

[0027] In the present invention, the recycled or renewable organic material is typically selected from the group consisting of plant-based fats and oils, animal-based fats and oils, fossil waste-based oils, waste oils, seaweed oils, and microbial oils.

[0028] Specific examples of the recycled or renewable organic materials of the present invention include, but are not limited to, for example, animal-based fats and oils such as suet, tallow, fat, lard, whale oil, butterfat, fish oil, poultry oil and poultry fat; plant-based fats and oils such as, for example, palm oil sludge, rapeseed oil, canola oil, colza oil, sunflower oil, soybean oil, hempseed oil, olive oil, linseed oil, cottonseed oil, mustard oil, palm oil, peanut oil, castor oil, and coconut oil, lignocellulosic pyrolysis liquid (LPL), HTL-bio crude, crude tall oil (CTO), tall oil pitch (TOP), crude fatty acid (CFA), tall oil fatty acid (TOFA) and distilled tall oil (DTO); microbial oils; seaweed oils; recycled fats from the food industry such as, for example, used cooking oil, yellow and brown greases or various waste streams; any lipid containing free fatty acids, phosphorus and / or metals, oils derived from yeast or fungal products, recycled dietary fats; starting materials produced by genetic engineering, as well as any mixture of such feedstocks.

[0029] In one embodiment of the present invention, the recycled or renewable organic material is selected from the group consisting of tall oil derivatives and pyrolysis oils, particularly, tall oil pitch (TOP), hydrothermal liquefaction oil (HTL), lignocellulosic pyrolysis oil, AF oil, used crude oil (UCO), used lubricating oil (ULO), waste plastic pyrolysis oil (WPPO), pyrolysis oil from waste tire (ELT), seaweed oil, and lignin oil, more particularly, the recycled or renewable organic material is tall oil pitch (TOP).

[0030] In particular, recycled or renewable organic materials include tall oil pitch (TOP).

[0031] The recycled or renewable organic material processed by the method of the present invention contains a large amount of silicon compound. The recycled or renewable organic material of the present invention contains more than 1 ppm of silicon compound. In particular, the recycled or renewable organic material of the present invention contains more than 10 ppm of silicon compound, more particularly, the recycled or renewable organic material of the present invention contains more than 15 ppm of silicon compound, and even more particularly, the recycled or renewable organic material of the present invention contains more than 20 ppm of silicon compound.

[0032] The recycled or renewable organic materials processed by the method of the present invention further contain a large amount of phosphorus compounds. The phosphorus compounds present in the biomass-based lipid material are typically phospholipids, and the phospholipids present in the biomass-based lipid material are, in particular, one or more of phosphatidylethanolamine, phosphatidylcholine, phosphatidylinositol, phosphatidic acid, and phosphatidylethanolamine.

[0033] In particular, the recycled or renewable organic material of the present invention contains 1 to 1000 ppm of phosphorus as a phosphorus compound.

[0034] The recycled or renewable organic materials processed by the method of the present invention contain a large amount of chloride (Cl). Typically, the chloride exists in the form of chloride salts and / or organic chloride compounds such as chlorinated hydrocarbons. The recycled or renewable organic materials of the present invention contain more than 20 ppm of Cl, particularly more than 50 ppm of Cl, and more particularly 50 to 1000 ppm of Cl. Furthermore, the recycled or renewable organic materials processed by the method of the present invention contain a large amount of oxygen as organic oxygen compounds.

[0035] The recycled or renewable organic materials processed by the method of the present invention may also contain further impurities, such as impurities containing phosphorus and / or metals in the form of phospholipids, soaps and / or salts. The impurities may be, for example, phosphates or sulfates, iron salts or organic salts, soaps or phospholipids. Metallic impurities that may be present in biomass-based lipid materials 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.

[0036] Accordingly, a method for purifying recycled or renewable organic material is provided herein, wherein the recycled or renewable organic material contains one or more impurities selected from the group consisting of silicon compounds, phosphorus compounds, chlorine compounds, nitrogen compounds, sulfur compounds and hydroxyaromatic compounds, and the method is provided to obtain a purified, hydrogenated recycled or renewable organic material. (a) A process of providing recycled or renewable organic materials, (b) optionally preheating the recycled or renewable organic material at 180-325°C, optionally adding an acid before or after the preheating process, and optionally filtering the preheated recycled or renewable organic material after preheating. (c) A step of heating recycled or renewable organic material at a temperature of 150 to 450°C, optionally in the presence of an adsorbent, optionally adding water before or during the heating process, optionally adding an acid before or after the heating process, and optionally filtering the heated recycled or renewable organic material after the heating process. (d) optionally, a step of evaporating volatile silicon compounds from heat-treated recycled or renewable organic material, thereby reducing the silicon content of the heat-treated recycled or renewable organic material. (e) optionally, a process of pyrolysis of the recycled or renewable organic material to reduce the oxygen and phosphorus content of the heat-treated recycled or renewable organic material, optionally removing volatile substances from the pyrolysis of the recycled or renewable organic material, and optionally removing solids / sediments from the recycled or renewable organic material. (f) A process of hydrogenating a heat-treated recycled or renewable organic material in the presence of a hydrogenation catalyst. Includes.

[0037] Prior to the heat treatment in step (c), the recycled or renewable organic material may be subjected to a preheat treatment in the absence of an adsorbent material. In an optional step (b), the recycled or renewable organic material is heated to induce a thermal reaction that breaks down silicon-containing impurities contained in the recycled or renewable organic material, producing volatile silicon compounds that can then be removed from the recycled or renewable organic material. Specifically, polydimethylsiloxane (PDMS) resulting from the anti-contamination agent decomposes into volatile polydimethylcyclosiloxane (PDMCS) under the treatment conditions.

[0038] The heat treatment in step (b) is carried out at any temperature between 180 and 325°C. To achieve ideal results, step (b) is carried out at 200 to 300°C, preferably 240 to 280°C.

[0039] The time during which the recycled or renewable organic material is heated and maintained at a desired temperature, i.e., the residence time, is typically 1 to 300 minutes, preferably 5 to 90 minutes, and more preferably 20 to 40 minutes, in step (b).

[0040] The pressure during the heat treatment in step (b) is typically 500 to 5000 kPa, preferably 800 to 2000 kPa.

[0041] Optionally, the process may be further accelerated by adding an acid before or after the preheating treatment in step (b). This removes any remaining sodium impurities. The acid is preferably selected from citric acid and phosphoric acid.

[0042] In step (b), adsorbents containing solid materials and / or undesirable impurities resulting from the heat treatment can be removed. Removal of solid materials can be achieved by any separation method that is understood to be appropriate to those skilled in the art for separating solid materials from heat-treated recycled or renewable organic materials. Suitable examples include, but are not limited to, filtration, centrifugation, and phase separation. It should be understood that several separation methods, such as filtration and centrifugation, can be combined. Preferably, removal is achieved by filtration. Removal is preferably carried out at any temperature between 100 and 180°C.

[0043] Removing solids / sediments prevents deactivation of the hydrogenation catalyst in the hydrogenation of recycled or renewable organic materials.

[0044] In step (c), the recycled or renewable organic material is heated to any temperature between 100 and 450°C. To achieve ideal results, step (c) is carried out at 180 to 325°C, preferably 200 to 300°C, and more preferably 240 to 280°C.

[0045] The time during which the recycled or renewable organic material is heated and maintained at a desired temperature, i.e., the residence time, is typically 1 to 300 minutes, preferably 5 to 240 minutes, and more preferably 30 to 90 minutes in step (c).

[0046] The pressure in process (c) is typically 500 to 5000 kPa, preferably 800 to 2000 kPa.

[0047] In step (c), the recycled or renewable organic material is heated to induce a thermal reaction that breaks down the structure of impurity-containing compounds present in the recycled or renewable organic material, resulting in the formation of material adsorbed onto an adsorbent present in heating step (c), or a solid precipitate, and thus material that can be subsequently removed from the recycled or renewable organic material.

[0048] Optionally, an adsorbent is present in step (c). The adsorbent present in step (c) may be selected from silica-based adsorbents. Preferably, the adsorbent is selected from the group consisting of aluminum silicate, silica gel, and mixtures thereof. In step (c), the amount of adsorbent is typically 0.1 to 10.0 wt%, preferably 0.5 to 2.0 wt%, of the total weight of the processed recycled or renewable organic material.

[0049] In step (c), adsorbents containing solid materials and / or undesirable impurities resulting from the heat treatment can be removed. Removal of solid materials can be achieved by any separation method that is understood to be appropriate to those skilled in the art for separating solid materials from heat-treated recycled or renewable organic materials. Suitable examples include, but are not limited to, filtration, centrifugation, and phase separation. It should be understood that several separation methods, such as filtration and centrifugation, can be combined. Preferably, removal is achieved by filtration. Removal is preferably carried out at any temperature between 100 and 180°C.

[0050] Removing solids / sediments prevents deactivation of the hydrogenation catalyst in the hydrogenation of recycled or renewable organic materials.

[0051] In particular, if an adsorbent is present in step (c), it is preferentially removed. Therefore, optionally, after heat treatment, adsorbents containing undesirable impurities are removed. Thus, in step (c), the recycled or renewable organic material is subjected to the removal of solid adsorbent material. The removal of solid material can be achieved by any separation method that is understood to be appropriate to those skilled in the art for separating solid material from heat-treated recycled or renewable organic material. Appropriate examples include, but are not limited to, filtration, centrifugation, and phase separation. It should be understood that several separation methods, such as filtration and centrifugation, may be combined. Preferably, removal is achieved by filtration. Removal is preferably carried out at any temperature between 100 and 180°C.

[0052] Optionally, the process may be further accelerated by adding an 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.

[0053] Furthermore, optionally, in step (c), the process may be accelerated by adding water to the material before or during the heat treatment process. In step (c), the moisture content in the feed, i.e., the recycled or renewable organic material, may vary predominantly between 500 and 5000 ppm. If the recycled or renewable organic material contains more than 5000 ppm of water, it may be removed from the feed before step (c) by any suitable method known to those skilled in the art to reduce the moisture content in the recycled or renewable organic material to less than 5000 ppm.

[0054] For example, the recycled or renewable organic material provided in step (a) containing more than 20 ppm of Cl may be heated in the presence of an aqueous alkali metal hydroxide at a temperature of 100 to 450°C to obtain a purified recycled or renewable organic material containing less than 50% of the original chlorine content of the recycled or renewable organic material provided in step (a) (step c1).

[0055] In step (c1), the recycled or renewable organic material is heated to produce a thermal reaction that decomposes chlorine-containing impurities, particularly chlorinated organic hydrocarbons. The heat treatment in step (c1) is carried out at any temperature between 100 and 450°C. To achieve ideal results, step (c1) is carried out at 150 to 400°C, preferably between 200 and 300°C.

[0056] With respect to step (c1), the time during which the recycled or renewable organic material is heated and maintained at a desired temperature, i.e., the residence time, is typically 1 to 180 minutes, preferably 2 to 90 minutes, and more preferably 5 to 60 minutes in step (c1).

[0057] The alkali metal hydroxide is typically selected from the group consisting of KOH, LiOH, NaOH, and mixtures thereof. The alkali metal hydroxide is preferably NaOH. The concentration of the alkali metal hydroxide in aqueous solution is typically 0.1 to 10.0 mol / L. The ratio of the aqueous solution of alkali metal hydroxide to the treated recycled or renewable organic material in step (c1) is typically greater than 0.1 g / g, and preferably 0.5 to 1.5 g / g.

[0058] After heating, the organic and aqueous fractions can be separated by appropriate methods known to those skilled in the art to obtain a purified recycled or renewable organic material containing less than 50% of the chlorine content of the recycled or renewable organic material provided in step (a).

[0059] Alternatively, step (c) may be achieved by heat-treating the recycled or renewable organic material at a temperature between 250 and 450°C, preferably between 350 and 450°C, to obtain a heat-treated recycled or renewable organic material (step (c2)).

[0060] Alternatively, step (c) may be achieved by heat-treating the recycled or renewable organic material at a temperature of preferably 180-325°C to form a heat-treated recycled or renewable organic material (step (c3)), where at least some of the silicon compounds present in the recycled or renewable organic material are converted into volatile silicon compounds.

[0061] In step (c3), the recycled or renewable organic material is heated to induce a thermal reaction that breaks down silicon-containing impurities present in the recycled or renewable organic material, producing volatile silicon compounds that can then be removed from the heat-treated recycled or renewable organic material. Specifically, polydimethylsiloxane (PDMS) resulting from the anti-contamination agent decomposes into volatile polydimethylcyclosiloxane (PDMCS) under the treatment conditions.

[0062] The heat treatment in step (c3) is typically carried out at any temperature between 180 and 325°C. To achieve ideal results, step (c3) is carried out at 200 to 300°C, preferably 240 to 280°C.

[0063] The time during which the recycled or renewable organic material is heated and maintained at a desired temperature, i.e., the residence time, is typically 1 to 300 minutes, preferably 5 to 90 minutes, and more preferably 20 to 40 minutes, in step (c3).

[0064] The pressure during the heat treatment in step (c3) is typically 500 to 5000 kPa, preferably 800 to 2000 kPa.

[0065] The pressure range in process (c3) is influenced by the volatility of water, and it is particularly advantageous to maintain a heat treatment pressure slightly higher than the equilibrium pressure of water boiling at the heat treatment temperature. Pressures that are too low will cause volatile compounds to act like water and push the fatty acid fraction into the gas phase. Carryover of organic volatiles is increased by the presence of water or stripping.

[0066] The applicable step (c3) preferably provides a purified recycled or renewable organic material that contains less silicon than the recycled or renewable organic material provided in step (a), preferably less than 10%, more preferably less than 5%, and even more preferably less than 1% of the original silicon content of the recycled or renewable organic material provided in step (a).

[0067] In a further embodiment, step (c) is achieved by heating the recycled or renewable organic material at any temperature between 180 and 325°C in the presence of an adsorbent (step (c4)). To achieve ideal results, step (c4) is carried out at 200 to 300°C, preferably 240 to 280°C.

[0068] The time during which the recycled or renewable organic material is heated and maintained at a desired temperature, i.e., the residence time, in step (c4) is typically 1 to 300 minutes, preferably 5 to 240 minutes, and more preferably 30 to 90 minutes.

[0069] In step (c4), the recycled or renewable organic material is heated to induce a thermal reaction that breaks down the structure of impurity-containing compounds contained in the recycled or renewable organic material, resulting in the formation of material that is adsorbed onto the adsorbent present in heating step (c), or a solid precipitate, and thus material that can be subsequently removed from the recycled or renewable organic material.

[0070] The adsorbent present in step (c4) may be selected from silica-based adsorbents. Preferably, the adsorbent is selected from the group consisting of aluminum silicate, silica gel, and mixtures thereof. In step (d4), the amount of adsorbent is typically 0.1 to 10.0 wt%, preferably 0.5 to 2.0 wt%, of the total weight of the processed recycled or renewable organic material.

[0071] An applicable step (c4) is preferably to provide a purified recycled or renewable organic material containing less than 30% of the original phosphorus content of the recycled or renewable organic material provided in step (a).

[0072] Following the heat treatment in step (c), volatile substances generated as a result of the heat treatment or present in the heat-treated recycled or renewable organic material are removed. Thus, in an optional step (d), the heat-treated recycled or renewable organic material is subjected to the evaporation of volatile silicon compounds from the heat-treated recycled or renewable organic material in one or more steps. In step (d), evaporation is achieved at any temperature, predominantly 145–250°C, and particularly 150–225°C. To achieve ideal results, evaporation in step (d) is carried out at a temperature of 160–200°C, preferably 160–180°C.

[0073] The reduced pressure in step (d) is such that evaporation of the volatile Si compound is achieved. Typically, the pressure is 0.1 to 5 kPa, preferably 0.1 to 3 kPa.

[0074] The evaporated weight should be adjusted to 1-10 wt%, preferably 1-8 wt%, more preferably 1-5 wt%, and even more preferably 1-3 wt%, of the heat-treated recycled or renewable organic material.

[0075] Furthermore, it is preferable to add water to the initial mixture of heat-treated recycled or renewable organic materials. Adding a small percentage of water to the initial heat-treated recycled or renewable organic materials allows the use of lower temperatures and higher vacuum pressures while achieving the same level of Si removal compared to normal evaporation. More importantly, there is only less loss of volatile fatty acids, which reduces the amount of fatty acid waste by half compared to evaporation without water.

[0076] Therefore, in one embodiment of the present invention, water is added to the heat-treated recycled or renewable organic material, and thus the water content before the evaporation step (d) is 1 to 5 wt%, preferably 1.5 to 4 wt%, more preferably 2 to 3 wt%, of the total weight of the heat-treated recycled or renewable organic material.

[0077] The applicable step (d) provides a vapor fraction comprising a major portion which is a volatile silicon compound, and 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).

[0078] Evaporation in step (d) can be achieved by any evaporation method deemed appropriate by those skilled in the art for the separation of volatile substances from heat-treated recycled or renewable organic materials. Suitable examples include, but are not limited to, falling thin-film evaporation, rising film evaporation, thin-film evaporation, and flash evaporation. Evaporation can be achieved 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. The preferred evaporation method of the present invention is one-stage or multi-stage flash evaporation. Due to the high pressure difference in the flash chamber, flash evaporation requires less evaporation to provide better mass transfer compared to thin-film evaporation. For example, applying the same methods and equipment as in a typical thin-film evaporation process of crude tall oil (CTO) for tall oil pitch (TOP) after heat treatment results in significantly increased heat consumption compared to flash evaporation.

[0079] The ideal temperature, pressure, mass to be evaporated, and number of flash stages used depend on the composition and quality of the recycled or renewable organic material, as well as the heat treatment parameters (temperature, pressure, and residence time) of process (c).

[0080] Following the desired heat treatment and the optional evaporation of volatile silicon compounds, the heat-treated recycled or renewable organic material may be subjected to further purification by thermal decomposition.

[0081] In an optional step (e), the recycled or renewable organic material is heated to induce thermal decomposition that breaks down phosphorus compounds contained in the recycled or renewable organic material, thereby producing a solid material from the heat-treated recycled or renewable organic material that can subsequently be removed, for example, by filtration.

[0082] The pyrolysis in step (b) may be carried out in a separate reactor unit or in a hydrogenation reactor prior to the catalyst bed in a guard bed.

[0083] Therefore, in step (e), the recycled or renewable organic material is thermally decomposed, thereby reducing the oxygen content and phosphorus content of the recycled or renewable organic material.

[0084] The thermal decomposition in step (e) is typically carried out at any temperature between 350 and 450°C.

[0085] The pyrolysis in step (e) is carried out in an apparatus that allows for a sufficient residence time. The time during which the recycled or renewable organic material is heated and maintained at a desired temperature, i.e., the residence time, in step (e) is typically 1 to 300 minutes, preferably 5 to 240 minutes, and more preferably 30 to 90 minutes.

[0086] The pressure in process (e) is such that sufficient oxygen removal is achieved. Typically, the pressure in process (e) is 4 to 20 MPa, preferably 8 to 16 MPa.

[0087] Following the thermal decomposition in step (e), volatile substances generated as a result of thermal differentiation or present in the recycled or renewable organic material may be removed. Thus, in step (e), the thermally decomposed recycled or renewable organic material may optionally be subjected to a step to remove volatile substances from the thermally decomposed recycled or renewable organic material. This may be carried out in one or more steps. Typical examples of volatile substances include CO and CO2.

[0088] The removal of volatile substances can be achieved by any separation method that is understood to be suitable to those skilled in the art, for example, for separating volatile substances from thermally decomposed recycled or renewable organic materials. Suitable examples include, but are not limited to, evaporation, particularly flash evaporation and thin-film evaporation.

[0089] The optimal temperature, pressure, mass evaporated, and number of flash stages used depend on the composition and quality of the recycled or renewable organic material, as well as the thermal decomposition parameters (temperature, pressure, and residence time) of process (e).

[0090] The temperature and pressure in the volatile matter removal step (e) are such that evaporation of volatile oxygen compounds is achieved. In step (e), volatile matter removal is typically achieved at any temperature between 300 and 450°C. To achieve ideal results, volatile matter removal in step (e) is carried out at 350 to 450°C, and typically the pressure in volatile matter removal in step (e) is 0.1 to 5 kPa, preferably 0.1 to 3 kPa.

[0091] Removing volatile substances reduces the amount of oxygen in recycled or renewable organic materials.

[0092] Following the pyrolysis in step (e), any solid material generated as a result of the pyrolysis may be removed. Thus, in step (e), the pyrolyzed recycled or renewable organic material may optionally be subjected to a step to remove solids / sediments from the pyrolyzed recycled or renewable organic material.

[0093] The removal of solid materials can be achieved by any separation method that is understood to be suitable to those skilled in the art, for example, for separating solid materials from pyrolyzed recycled or renewable organic materials. Suitable examples include, but are not limited to, filtration, centrifugation, bleaching, degumming, and phase separation. It should also be understood that several separation methods, such as filtration and centrifugation, can be combined. Preferably, removal is achieved by filtration. Removal is preferably carried out at any temperature between 100 and 180°C.

[0094] Removal of solids / precipitates, particularly those containing phosphorus, helps avoid deactivation of hydrogenation catalysts in the hydrogenation of recycled or renewable organic materials.

[0095] The applicable step (e) preferably provides a purified recycled or renewable organic material fraction containing less than 30% of the original phosphorus content of the recycled or renewable organic material provided in step (iv) (a).

[0096] After step (c), the purified recycled or renewable organic material is subjected to hydrogenation (f) to further remove Cl from the recycled or renewable organic material.

[0097] The term "hydrotreating" refers to a chemical engineering process in which hydrogen reactions are used, particularly as part of oil refining, to remove impurities such as oxygen, sulfur, nitrogen, phosphorus, silicon, and metals.

[0098] Hydrogenation can be carried out in one or more steps in one or more reactor units or catalyst beds.

[0099] Process (f) is typically achieved under a sustained hydrogen flow. To achieve ideal results, the sustained hydrogen flow in process (f) has an H2 / feed ratio of 500–2000 n-L / L, more preferably 800–1400 n-L / L.

[0100] In step (f), the hydrogenation treatment is preferably carried out at a temperature of 270 to 380°C, more preferably 275 to 350°C, and more preferably 300 to 330°C. Typically, the pressure in step (f) is 4 to 20 MPa.

[0101] The hydrogenation catalyst in step (f) preferably comprises at least one component selected from group 6, 8, or 10 of the IUPAC periodic table. Preferably, the hydrogenation catalyst in step (f) is a supported Pd, Pt, Ni, NiW, NiMo, or CoMo catalyst, and the support is a zeolite, zeolite-alumina, alumina, and / or silica, preferably NiMo / Al2O3 or CoMo / Al2O3. In particular, the hydrogenation catalyst is a NiW, NiMO, or CoMo sulfide catalyst.

[0102] The time during which the recycled or renewable organic material is heated and maintained at a desired temperature, i.e., the residence time, is typically 1 to 300 minutes, preferably 5 to 240 minutes, and more preferably 30 to 90 minutes in step (e).

[0103] An applicable hydrogenation step (f) provides a purified, hydrogenated recycled or renewable organic material, wherein the purified, hydrogenated recycled or renewable organic material contains (i) less than 10%, preferably less than 5%, more preferably less than 1% of the original silicon content of the recycled or renewable organic material provided in step (a), and / or (ii) less than 30% of the original phosphorus content of the recycled or renewable organic material provided in step (a), and / or (iii) less than 20 ppm of chlorine or less than 50% of the chlorine content of the recycled or renewable organic material provided in step (a), and / or (iv) less than 30% of the original phosphorus content of the recycled or renewable organic material provided in step (a).

[0104] In certain embodiments, step (f) is achieved by step (f1) of hydrodeoxygenation (HDO) of a heat-treated recycled or renewable organic material fraction. This is preferably carried out in the presence of an HDO catalyst, at a temperature of 270–380°C, at a pressure of 4–20 MPa, and under a continuous hydrogen stream. Preferably, step (f1) is carried out to obtain a purified recycled or renewable organic material containing less than 1 wt% oxygen.

[0105] The term "hydrodeoxygenation (HDO)" refers to the removal of oxygen as water through the action of hydrogen molecules under the influence of an HDO catalyst.

[0106] The HDO catalyst may be selected from the group consisting of, for example, NiMO-, CoMo-, NiW- catalysts and any mixture thereof. Preferably, the HDO catalyst in step (f) is a NiW sulfide, NiMo sulfide, or NiMO sulfide catalyst.

[0107] Advantageously, a sustained hydrogen flow has an H2 / feed ratio of 500-2000 n-L / L, preferably 800-1400 n-L / L.

[0108] To achieve ideal results, some of the hydrogenated recycled or renewable organic material may be recycled back into process (f1). Preferably, the ratio of fresh feed, i.e., the purified recycled or renewable organic material obtained in process (f1), to the recycled, hydrogenated recycled or renewable organic material is 2:1 to 20:1.

[0109] If step (f) is achieved by step (f1) of hydrodeoxygenating (HDO) a heat-treated fraction of recycled or renewable organic material at a temperature of 290 to 350°C, under a pressure of 4 to 20 MPa, and under a continuous flow of hydrogen in the presence of an HDO catalyst, then a purified recycled or renewable organic material is obtained that preferably contains less than 1 wt% oxygen and / or less than 20% of the original silicon content of the recycled or renewable organic material provided in step (a), preferably less than 10%, more preferably less than 5%, and / or less than 30% of the original phosphorus content of the recycled or renewable organic material provided in step (a), and / or less than 50% of the chlorine content of the recycled or renewable organic material provided in step (a).

[0110] In another embodiment, step (d) is achieved by (d2) hydrodesulfurizing (HSD) a heat-treated recycled or renewable organic material fraction. The term "hydrodesulfurization (HDS)" means the removal of sulfur as hydrogen sulfide by the action of hydrogen molecules under the influence of a (HDS) catalyst.

[0111] In another embodiment, step (d) is achieved by (d3) hydrogenation metallization (HDM) of a heat-treated recycled or renewable organic material fraction. The term "hydrodemetallization (HDM)" means the removal of metal by trapping it using an (HDM) catalyst.

[0112] In another embodiment, step (d) is achieved by (d4) hydrogen denitrification (HDN) of a heat-treated recycled or renewable organic material fraction. The term "hydrodenitrification (HDN)" means the removal of nitrogen by the action of hydrogen molecules under the influence of an (HDN) catalyst.

[0113] In another embodiment, step (d) is achieved by (d5) hydrodearomatization (HDA) of a heat-treated recycled or renewable organic material. The term "hydrodearomatization (HDA)" means saturation or ring-opening of an aromatic compound by the action of hydrogen molecules under the influence of a catalyst.

[0114] Figure 1 shows a first exemplary process flow of the method of the present invention.

[0115] Referring to Figure 1, a feed of recycled or renewable organic material, specifically tall oil pitch (TOP), 10, is subjected to a preheat treatment 20 of the recycled or renewable organic material to obtain a heat-treated recycled or renewable organic material fraction 21, as described herein as step (b). The preheat-treated recycled or renewable organic material 21 is then subjected to a heating 30 of the recycled or renewable organic material in the presence of an adsorbent to adsorb impurities and to allow the mixture to be separated, as described herein as step (c). The adsorbent is then separated from the treated feed of recycled or renewable organic material 40, as described in step (c), to obtain a purified recycled or renewable organic material 41 and an adsorbent 42 containing the main portion of impurities. The purified recycled or renewable organic material is then subjected to hydrogenation 50 as described herein as step (f) to obtain the purified, hydrogenated recycled or renewable organic material 51, wherein the purified, hydrogenated recycled or renewable organic material contains less than 50% of the impurity content of the recycled or renewable organic material provided in step (a). The purified, hydrogenated recycled or renewable organic material 51 may then be subjected to catalytic upgrading 60.

[0116] Figure 2 shows a first exemplary process flow of the method of the present invention.

[0117] Referring to Figure 2, the feed of recycled or renewable organic material, particularly tall oil pitch (TOP), 10, is subjected to a preheat treatment 20 of the recycled or renewable organic material, as described herein as step (b), in order to obtain a heat-treated recycled or renewable organic material fraction 21 containing less than 50% of the impurity content of the recycled or renewable organic material provided in step (a). The preheat-treated recycled or renewable organic material 21 is then subjected to a heat treatment 35 of the recycled or renewable organic material, as described herein as step (c). The heat-treated feed of recycled or renewable organic material is then evaporated 45, as described herein as step (c), to obtain a bottom fraction containing a heat-treated recycled or renewable organic material fraction 46 containing less than 30% of the original silicon content of the recycled or renewable organic material provided in step (a), and a vapor fraction 47 containing the main portion which is a volatile silicon compound. The purified, recycled, or renewable organic material is then subjected to hydrogenation deoxygenation 50, as described herein as step (d), to obtain the purified, deoxygenated recycled, or renewable organic material 51. The deoxygenated recycled, or renewable organic material 51 may then be subjected to catalytic upgrading 60.

[0118] After the recycled or renewable organic material has been purified according to the method of the present invention, it may be subjected to further processing, such as catalytic upgrading. Such catalytic upgrading processes include, but are not limited to, catalytic cracking, catalytic hydrogenation, thermal catalytic cracking, catalytic hydrogenation, fluid catalytic cracking, catalytic ketonation, and catalytic esterification. Such processes require that the recycled or renewable organic material is sufficiently pure and free of impurities, otherwise it may interfere with the catalytic process or contaminate the catalyst present in the process.

[0119] Accordingly, the present invention further provides a process for producing recycled or renewable hydrocarbons, comprising: (x) purifying a recycled or renewable organic material as described herein; and (y) subjecting the purified recycled or renewable organic material to an essential oil conversion process, wherein the essential oil conversion process includes steps to change the molecular weight of the feed, such as hydrocracking or steam cracking; remove heteroatoms from the feed, such as thermal catalytic cracking, fluid catalytic cracking or hydrogenation, particularly hydrodesulfurization or hydrodesulfurization; change the degree of saturation of the feed, such as hydrogenation, thermal catalytic cracking or fluid catalytic cracking; rearrange the molecular structure of the feed, such as isomerization; or any combination thereof, in order to obtain at least one recycled or renewable hydrocarbon.

[0120] In a typical embodiment of the process of the present invention, the recycled or renewable hydrocarbon is a renewable traffic fuel or fuel component.

[0121] In one embodiment of the process of the present invention, step (y) is hydrocracking. In such an embodiment, step (y) is preferably carried out in a mild hydrocracking (MHC) refinery unit, particularly in the presence of a hydrocracking catalyst.

[0122] In another embodiment of the process of the present invention, step (y) is steam decomposition. In such an embodiment, step (y) is preferably carried out in a steam decomposition unit.

[0123] In yet another embodiment of the process of the present invention, step (y) is isomerization. In such an embodiment, step (y) is preferably carried out in an isomerization unit.

[0124] In yet another embodiment of the process of the present invention, step (y) is a hydrogenation treatment. In such an embodiment, step (y) is preferably carried out in a hydrogenation treatment unit.

[0125] In yet another embodiment of the process of the present invention, step (y) is thermal catalytic decomposition (TC). In such embodiments, step (y) is preferably carried out in a thermal catalytic decomposition unit.

[0126] In yet another embodiment of the process of the present invention, step (y) is fluid catalytic cracking (FCC). In such an embodiment, step (y) is preferably carried out in a fluid catalytic cracking unit. [Examples]

[0127] Example 1 Crude and heat-treated tall oil pitch (TOP) was subjected to distillation under various conditions. The yields and silicon content of the resulting distillates and bottom fractions are shown in Table 1 (see reference) for crude TOP and Table 2 for heat-treated TOP.

[0128] [Table 1]

[0129] [Table 2]

[0130] As is evident from Tables 1 and 2, the silicon content in the bottom fraction of heat-treated TOP is significantly lower compared to that of crude TOP.

[0131] Example 2 Six tall oil pitch qualities were flash-evaporated with and without water (3%). Process conditions are shown in Table 3 (without water) and Table 4 (with water).

[0132] [Table 3]

[0133] [Table 4]

[0134] [Table 5]

[0135] With and without water addition, the average Si removal efficiency of flash evaporation was 73% across all six top-quality samples tested (Table 5). More importantly, there was only less loss of volatile fatty acids, which reduced the amount of fatty acid waste by half compared to flushing without water (Table 4).

[0136] Example 3 Heat-treated and flash-evaporated TOP samples were hydrogenated (hydrogenated deoxygenated) at various temperatures. Other process conditions, pressure, and weight-to-space velocity (WHSV) were kept constant. The pressure was 5000 kPa and the WHSV was 0.95 1 / h.

[0137] TIFF0007911840000006.tif30152

[0138] The Si removal efficiency of hydrogenation in heat-treated and flash-evaporated TOP increases with increasing temperature (Table 6).

[0139] Example 4: High-temperature NaOH treatment of waste plastic pyrolysis oil The following experiment was conducted in a 1-liter batch autoclave reactor. 340 g of waste plastic pyrolysis oil and 2 wt% aqueous NaOH (227 g) were weighed together into the reactor container. After sealing and pressure testing, the reactor, circulating at 500 ppm, was heated to the desired reaction temperature of 240°C, which was then maintained for 30 minutes. The reactor was then cooled to room temperature before product collection. The contents were poured from the reactor container into a centrifuge tube using a slanted method, and the liquid was centrifuged at 20°C and 4300 rpm for 30 minutes. After centrifugation, the purified pyrolysis oil was collected as a separation layer, and its Cl, Br, S, and N content was analyzed. Cl, Br, and S content was measured by X-ray fluorescence analysis, and N content was determined according to the ASTM D5762 standard. The results shown in Table 7 clearly demonstrate a reduction of more than 60% in both Cl and Br content.

[0140] [Table 6]

[0141] Example 5 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 wt%. Crude TOP samples from various manufacturers were tested. 0.4 wt% water was added before the high-temperature adsorption treatment.

[0142] During the high-temperature adsorption treatment, the sample material was heated to a temperature of 280°C for 60 minutes. After this treatment, the sample material was cooled to 100°C and then filtered using 0.45 μm filter paper.

[0143] The results suggest that Si and other impurities can be removed very efficiently from the feed at high temperatures, in the presence of either aluminum silicate or silica gel adsorbents. However, more efficient purification was achieved using silica gel adsorbents. The results are shown in Table 8. As is clear from Table 9 and Figures 3 and 4, efficient removal of Si and P cannot be achieved by simple acid + heat treatment or acid + adsorption purification methods.

[0144] [Table 7] TIFF0007911840000009.tif55128

[0145] [Table 8]

[0146] To those skilled in the art, it will be apparent that, with advances in the technology, the concept of the invention can be implemented in various ways. The present invention and its embodiments may be modified within the scope of the claims without being limited to the examples described above.

Claims

1. A method for purifying renewable organic material, wherein the renewable organic material is selected from the group consisting of plant-based fats and oils, animal-based fats and oils, seaweed oils, and microbial oils, and contains one or more impurities selected from the group consisting of silicon compounds, phosphorus compounds, chlorine compounds, nitrogen compounds, sulfur compounds, and hydroxyaromatic compounds, and the renewable organic material contains more than 1 ppm of silicon compounds, and the method obtains a purified, hydrogenated renewable organic material containing less than 20% of the original silicon content of the renewable organic material provided in step (a) below, (a) A process for providing renewable organic materials, (c) A step of heat-treating the renewable organic material at a temperature of 240 to 280°C and a pressure of 800 to 2000 kPa, wherein at least a portion of the silicon compound in the renewable organic material is converted into a volatile silicon compound. (d) (i) Vapor fraction containing a major portion which is a volatile silicon compound, and (ii) A heat-treated renewable organic material fraction containing less silicon than the renewable organic material provided in step (a) above. To obtain the above, the process involves evaporating the volatile silicon compound from the heat-treated renewable organic material compound at a temperature of 150 to 225°C and a pressure of 0.1 to 5 kPa, thereby reducing the silicon content of the heat-treated renewable organic material, and (f) A step of hydrogenating the heat-treated renewable organic material in the presence of a hydrogenation catalyst. A method that includes this.

2. (b) A step of preheating the renewable organic material at 180 to 325°C. The method according to claim 1, further comprising:

3. The method according to claim 2, wherein step (b) includes adding an acid before or after the preheating process.

4. The method according to claim 2 or 3, wherein step (b) comprises filtering the preheated regenerative organic material after the preheating treatment.

5. The method according to any one of claims 1 to 4, wherein step (c) is performed in the presence of an adsorbent.

6. The method according to any one of claims 1 to 5, wherein step (c) includes adding water before or during the heat treatment process.

7. The method according to any one of claims 1 to 6, wherein step (c) is a step of adding an acid before or after the heat treatment process.

8. The method according to any one of claims 1 to 7, wherein step (c) comprises filtering the heat-treated renewable organic material after the heat treatment.

9. (e) A step of thermally decomposing the renewable organic material, thereby reducing the oxygen and phosphorus content of the heat-treated renewable organic material. The method according to any one of claims 1 to 8, further comprising:

10. The method according to claim 9, wherein step (e) includes a step of removing volatile substances from the thermally decomposed renewable organic material.

11. The method according to claim 9 or 10, wherein step (e) includes the step of removing solids / sediments from the renewable organic material.

12. The method according to any one of claims 1 to 11, wherein in step (d), 1 to 10 wt% of the heat-treated renewable organic material is evaporated.

13. The method according to any one of claims 1 to 12, wherein water is added to the heat-treated renewable organic material, and the water content before the evaporation step (d) is 1 to 5 wt% of the total weight of the heat-treated renewable organic material.

14. The method according to claim 5, wherein the adsorbent in step (c) is selected from silica-based adsorbents.

15. The method according to claim 14, wherein the amount of the adsorbent in step (c) is 0.1 to 10.0 wt% of the total weight of the treated renewable organic material.

16. The method according to any one of claims 1 to 15, wherein, after step (d), the silicon content of the heat-treated renewable organic material fraction is less than 50% of the original silicon content of the renewable organic material provided in step (a).

17. The method according to any one of claims 1 to 16, wherein the hydrogenation treatment step (f) is carried out under a continuous flow of hydrogen.

18. The method according to claim 17, wherein the sustained hydrogen flow in step (f) has an H2 / feed ratio of 500 to 2000 n-L / L.

19. The method according to any one of claims 1 to 18, wherein step (f) is performed at a temperature of 270 to 380°C.

20. The method according to any one of claims 1 to 19, wherein step (f) is performed under a pressure of 4 to 20 MPa.

21. The method according to any one of claims 1 to 20, wherein the hydrogenation catalyst in step (f) comprises at least one component selected from group 6, 8, or 10 of the IUPAC in the periodic table.

22. The method according to any one of claims 1 to 21, wherein the hydrogenation catalyst in step (f) is a supported Pd, Pt, Ni, NiW, NiMo, or CoMo catalyst, and the support is a zeolite, zeolite-alumina, alumina, and / or silica.

23. The method according to any one of claims 1 to 22, wherein step (f) is achieved by a step (f1) of hydrodeoxygenating (HDO) the heat-treated renewable organic material fraction.

24. Step (f) is performed to obtain a purified renewable organic material containing less than 1 wt% oxygen and / or less than 20% of the original silicon content of the renewable organic material provided in step (a), (f1) A step of hydrogenating and deoxygenating (HDO) the heat-treated renewable organic material fraction at a temperature of 290 to 350°C, under a pressure of 4 to 20 MPa, and with a continuous flow of hydrogen in the presence of an HDO catalyst. The method according to claim 23, which is achieved by...

25. The method according to claim 23 or 24, wherein in step (f1), the HDO catalyst is a NiW sulfide, NiMo sulfide, or CoMo sulfide catalyst.

26. The method according to any one of claims 1 to 25, wherein a portion of the hydrogenated product is recycled to step (f).

27. The method according to claim 26, wherein the ratio of fresh feed to the hydrogenated product is 2:1 to 20:

1.

28. A process for producing renewable hydrocarbons, (x) A step of purifying a renewable organic material by the method described in any one of claims 1 to 27, and (y) A step of subjecting a purified renewable organic material to an essential oil conversion process, wherein the essential oil conversion process includes changing the molecular weight of the feed, removing heteroatoms from the feed, changing the degree of saturation of the feed, rearranging the molecular structure of the feed, or any combination thereof, in order to obtain at least one renewable hydrocarbon. A process that includes this.

29. The process according to claim 28, wherein the step (y) is hydrocracking.

30. Claim 29, wherein the above step (y) is performed in a mild hydrocracking (MHC) refinery unit. The process described.

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

32. The process according to claim 28, wherein the step (y) is steam decomposition.

33. The process according to claim 28, wherein the step (y) is isomerization.

34. The process according to claim 28, wherein the step (y) is a hydrogenation treatment.

35. The process according to claim 28, wherein the step (y) is thermal catalytic decomposition.

36. The process according to claim 28, wherein step (y) is fluid catalytic cracking.

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