EP4457324B1 - Verfahren zur herstellung von bioschmierölen - Google Patents

Verfahren zur herstellung von bioschmierölen

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Publication number
EP4457324B1
EP4457324B1 EP22844579.7A EP22844579A EP4457324B1 EP 4457324 B1 EP4457324 B1 EP 4457324B1 EP 22844579 A EP22844579 A EP 22844579A EP 4457324 B1 EP4457324 B1 EP 4457324B1
Authority
EP
European Patent Office
Prior art keywords
fatty acids
pipe
flow
polyalcohols
monoalcohols
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
EP22844579.7A
Other languages
English (en)
French (fr)
Other versions
EP4457324C0 (de
EP4457324A1 (de
Inventor
Martino Di Serio
Francesco Gallo
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Isuschem Srl
Itelyum Regeneration SpA
Original Assignee
Isuschem Srl
Itelyum Regeneration SpA
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Isuschem Srl, Itelyum Regeneration SpA filed Critical Isuschem Srl
Publication of EP4457324A1 publication Critical patent/EP4457324A1/de
Application granted granted Critical
Publication of EP4457324C0 publication Critical patent/EP4457324C0/de
Publication of EP4457324B1 publication Critical patent/EP4457324B1/de
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
    • C11C1/00—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids
    • C11C1/02—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids from fats or fatty oils
    • C11C1/04—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids from fats or fatty oils by hydrolysis
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M105/00—Lubricating compositions characterised by the base-material being a non-macromolecular organic compound
    • C10M105/08—Lubricating compositions characterised by the base-material being a non-macromolecular organic compound containing oxygen
    • C10M105/32—Esters
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B13/00—Recovery of fats, fatty oils or fatty acids from waste materials
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B13/00—Recovery of fats, fatty oils or fatty acids from waste materials
    • C11B13/02—Recovery of fats, fatty oils or fatty acids from waste materials from soap stock
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
    • C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
    • C11C3/003—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fatty acids with alcohols
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M2207/00—Organic non-macromolecular hydrocarbon compounds containing hydrogen, carbon and oxygen as ingredients in lubricant compositions
    • C10M2207/28—Esters
    • C10M2207/281—Esters of (cyclo)aliphatic monocarboxylic acids
    • C10M2207/2815—Esters of (cyclo)aliphatic monocarboxylic acids used as base material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M2207/00—Organic non-macromolecular hydrocarbon compounds containing hydrogen, carbon and oxygen as ingredients in lubricant compositions
    • C10M2207/40—Fatty vegetable or animal oils
    • C10M2207/401—Fatty vegetable or animal oils used as base material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10N—INDEXING SCHEME ASSOCIATED WITH SUBCLASS C10M RELATING TO LUBRICATING COMPOSITIONS
    • C10N2030/00—Specified physical or chemical properties which is improved by the additive characterising the lubricating composition, e.g. multifunctional additives
    • C10N2030/64—Environmental friendly compositions

Definitions

  • the present invention relates to a process for the production of lubricating biooils, starting from wastes of fat and surfactant substances.
  • the process of the present invention can be fully included in the so-called circular economy.
  • compulsory consortiums such as those for used oils, that take care of collecting waste substances directly from those that produce them.
  • a compulsory consortium for used edible oils receives all used fried oil from those who fry (restaurants, food industries and the like), which is no longer useful for cooking use due to the impurities that it contains and sometimes also to chemical composition modifications that can also make it dangerous for the health; the non-delivery of these wastes to the consortium may entail penalties for the negligent professional.
  • waste substances are often rich in materials that, with few, sometimes not even particularly complicated, treatments can provide starting or semifinished materials, which can then be used to make products having some market available, often with production costs even lower than those normally to be faced starting from primary starting materials.
  • the same energy and the same work are employed to get products that can be sold, often ever easily.
  • the so-called circular economy consists in this, allowing to reuse wastes deriving from the use of certain products to obtain other products.
  • processes for the regeneration of used mineral oils mainly lubricants for engines of various kinds are included with full rights, which, starting from wastes collected by related compulsory consortiums, obtain starting materials for lubricants, that are then sold to manufacturers of lubricants to produce end product lubricants, and bitumen, which is mainly used to asphalt roads, but that sometimes has also other uses, mainly in the field of inks. All these products are widely marketable and have a certain market, therefore these processes, in addition to allow to prevent the input of pollutants in the environment or their storage in places where they can be stored or burnt (with the risk of toxic smokes generation), allow those who practice them to get a certain income, triggering then a virtuous circle.
  • This process is particularly suitable for the recovery of mineral oils contaminated by esters of fatty acids derived from biofuels (biodiesel) or biooils (used as additives or mixed with lubricant oils due to a wrong collection management), reducing the number of stops due to clogging of the oven that feeds a subsequent column for fractioned distillation. Furthermore, such process allows to carry out other regeneration steps under milder conditions, allowing then further energy savings.
  • Esters produce considerable amounts of soap or surfactants, which still represent a fraction to be eliminated and do not allow to completely close the recycling cycle, leaving a fraction to be eliminated and that, in time, might gather up in the environment, with possible damage.
  • US 2020/0 224 121 discloses methods to treat residues of soap, in a way to generate free fatty acids and/or fatty acids derivatives, transforming basically all the soap residue into fatty acids. Feeding includes soap residues and saponifiable lipids.
  • WO 2009/158 379 discloses processes for the production of alkyl esters of fatty acids. It envisages to put into contact glycerides of fatty acids with alcohols, in the presence of a catalyst and to separate the reaction products from the catalyst and the alkyl esters of fatty acids from the reaction products.
  • Catalysts comprise a Periodic table group VIB metal, a group IIIA metal and a group VA element.
  • WO 2011/007 362 discloses a process to produce alkyl esters of fatty acids starting from one or more glycerol esters of the fatty acids or one or more fatty acids or a mixture thereof with an alcohol having 5 to 20 carbon atoms in the presence of a catalyst including oxides, mixed oxides, silicates, or sulphates of two or more of silicon, aluminium, iron, calcium, magnesium, sodium, and potassium.
  • EP 1 892 232 discloses a process for the production of esters of fatty acids and alcohols, comprising the steps of feeding fats with oils or fats of triglycerides, partial glycerides and/or free fatty acids; neutralising the charge by vacuum desorption at a temperature of 200 to 280°C, providing vapour and a residue; collecting a distillate from said vapour; transesterifying the residue with an alcohol including 1 to 5 carbon atoms with an alkaline catalyst; separating the transesterification mixture into an ester-containing fraction with 1 to 5 carbon atoms and an alcoholic fraction, a part of the free acids obtained being esterified with an alcohol in the presence of an acid catalyst, recycling the product in the feeding step.
  • the problem underlying the invention is to provide a recovery process for fat substances of different nature, which overcomes the disadvantages mentioned above and which allows safe disposal and enhances wastes of fatty nature.
  • This object is obtained by a process for the production of lubricating biooils starting from soaps, used cooking oils (UCO), animal fats, refined used cooking oils (RUCO), used biolubricants, wherein a soap acidification step and a hydrolysis step of the other waste to be regenerated is envisaged, in order to obtain fatty acids, characterised in that the products of these two steps are then reacted with monoalcohols and polyalcohols, to esterify them, to obtain lubricating biooils and solvents, and in that the reaction products of used mineral oils with a strong base are included among the soaps.
  • Dependent claims describe preferable features of the invention.
  • the present invention relates to a process for the production of lubricating biooils and solvents starting from some wastes, mainly fats and surfactants.
  • a feed 1 takes used cooking oils to a reactor 2, while a feed 3 takes water there.
  • feed 1 may also take waste biolubricants.
  • Reactor 2 is equipped with a stirrer 4, which can be a blade stirrer as illustrated, but it may also be of any other known type.
  • a further feed 5 carries zinc oxide (ZnO).
  • the reactor outputs a flow 6, that feeds a separator 7, which outputs two flows, one of product 8 and one 9, leading to a three-way valve 10.
  • the three-way valve 10 outputs a flow 11 and a flow 12.
  • the flow 12 feeds a tank 13, which outputs a flow 14 feeding a three-way valve 15, where also another flow 16 arrives.
  • a flow 17 starts from the three-way valve 15, which is a mixture of flows 14 and 16, that feeds a distillation column 18.
  • the distillation tail 19 contains product and the head 20 feeds a three-way valve 21; other two flows, 22 and 23, feed two tanks, 24 and 25 respectively.
  • a flow 26 starts from tank 24, which splits in two flows.
  • One flow 27 feeds a reactor 28, while a flow 29 feeds a distillation column 30.
  • Reactor 28, in addition to flow 27, is also fed with sulphuric acid from flow 31 and soaps from flow 32.
  • Reactor 28 outputs flow 33, that feeds a decanter tank 34.
  • Pipe 11 also merges into the pipe 33.
  • Flow 16 exits the decanter tank 34 and merges into the three-way valve 15, and with the product flow 35.
  • tank 25 in addition to pipe 23, also pipe 36 merges into it, including the distillation tails of column 30.
  • Tank 25 outputs flow 37 that merges into the three-way valve 38.
  • column 30 also outputs a head flow 39 feeding a tank 40, a pipe 41 that exits it merges into the three-way valve 38.
  • Reactor 43 in addition to flow 42, also receives flow 45, containing zinc oxide, flow 46, containing waste fatty acids and flow 47, coming from the three-way valve 48, where two flows merge, one, 49, containing 2-ethyl-hexanol and the other, 50, containing polyalcohols.
  • Reactor 43 outputs flow 51, feeding a separator 52, which outputs flow 53, that mixes with flow 5 entering the reactor 2, and one 54 feeding the three-way valve 55, which outputs two flows 56, 57.
  • Flow 56 feeds a tank 58, which outputs flow 59 feeding a reactor 60, while flow 57 feeds a tank 61, which outputs a product flow 62.
  • flow 63 containing hydrogen merges into reactor 60, while it outputs a product flow 64.
  • a hydrolysis reaction of used cooking oils takes place and, possibly of used biolubricants.
  • Zinc oxide coming both from feed 3, and from flow 53 -where it is present mainly as a zinc soap-, coming from the separator 52, is used as a catalyst for the process.
  • an oils/water/catalyst ratio between 100:40:1 and 200:50:5 by weight is used.
  • Temperature ranges from a minimum of 170°C to a maximum of 250°C; preferably, temperature ranges from 200 to 210°C.
  • a working pressure comprised between 10 and 30 bar is employed, preferably between 13 and 20 bar. With a reaction time between 3 and 10 hours, preferably between 5 and 8 hours, continuously, semi-continuously or batchwise.
  • Reactor 2 outputs, in flow 6, a mixture of water, and possibly raw glycerol -which can be advantageously used as a base for cosmetics- and/or polyalcohols, which can be used for other manufactures -in addition to the esterification step of the present process that will be disclosed later- and, anyway, that constitute one of the by-products of this process, and fatty acids.
  • Separator 7 separates water and possible raw glycerol and polyalcohols in flow 8 and fatty acids in flow 9.
  • Flow 9 is splitted in the three-way valve 10.
  • Flow 12 goes to tank 13, where the product is purified and sent, through flow 14, to the three-way valve 15.
  • the latter comes from reactor 28, where waste soaps - including reaction products of used mineral oils with a strong base- fed into 32, are acidified with sulphuric acid fed in 31, mentioned and described in the introduction.
  • the sulphuric acid/soap mixture has a ratio ranging from 1:3 to 3:1 by weight. Preferably, such ratio is 2:1.
  • As a sulphuric acid an aqueous solution of 70 g/l in concentration is generally used, which provides a suitable level of acidity, without damaging the plant, though.
  • Reaction temperature ranges between 50 and 150°C, preferably between 80 and 120°C. A particularly preferred temperature is 90°C.
  • the acidification reaction is carried out under an inert atmosphere, advantageously under nitrogen, in order to prevent side reactions that would lower the yield of the process.
  • Reaction time ranges between 0.5 and 4 hours, preferably between 1 and 2 hours.
  • Output flow 33 contains fatty acids, that mix up with those coming form flow 11, feeding then the decanter tank 34.
  • Output flow 35 from the decanter tank 34 contains water and salts, representing the only actual waste of the process according to the present invention, while purified fatty acids, through the pipe 16, are fed into the three-way valve 15.
  • a preliminary treatment thereof with hexane, and distillation can be foreseen, so obtaining the removal of residual oils, with a purer soap.
  • Pipe 17 exiting the three-way valve 15 leads to the distillation column 18. Its distillation tails, exiting through pipe 19, contain heavy fractions of fatty acids, as by-products. Heads, exiting through 20, are fed to the three-way valve 21, where the flow is splitted. Flow 22 goes to tank 24, that outputs flow 20, which goes to reactor 28 for admixing with acidified soaps, which are mainly fatty acids. From flow 20, though, pipe 29 leads a part of the purified fatty acids to the distillation column 30. Distillation tails go to tank 25, where distillation heads of column 18 have already arrived, while heads go to tank 40 through pipe 39. Distillation allows to begin the splitting into various final products, depending on their chemical formula, obviously according to their molecular weight.
  • Flows 41 and 37 arrived to the three-way valve 38, admix and, through pipe 42, are fed to reactor 43.
  • a first alcohol usually a monoalcohol, for example 2-ethyl-hexanol, fed in 49
  • a second alcohol usually a polyalcohol, for example trimethylol-propane, fed in 50, passing through pipe 47; optionally other fatty acids, fed in 46; and zinc oxide, fed in 45 arrive to reactor 43.
  • a first alcohol usually a monoalcohol, for example 2-ethyl-hexanol
  • a second alcohol usually a polyalcohol, for example trimethylol-propane, fed in 50, passing through pipe 47; optionally other fatty acids, fed in 46; and zinc oxide, fed in 45 arrive to reactor 43.
  • optionally other waste fatty acids in 46 is useful, according to a preferred embodiment, to adjust the viscosity of the final product.
  • fatty acids/alcohol/catalyst ratios range from 100:5:1 to 100:30:5 by weight; even preferably, they range from 100:10:1 to 100:20:3.
  • Temperature ranges from 150 to 300°C, preferably from 180 to 220°C.
  • Reaction time ranges from 2 to 8 hours, preferably from 4 to 6 hours. Water formed is preferably removed under vacuum.
  • Both natural alcohols such as ethanol and butanediol
  • synthetic alcohols such as 2-ethyl-hexanol, trimethylol-propane (TMP) and pentaerythritol
  • TMP trimethylol-propane
  • pentaerythritol can be used.
  • the esterified product is output from pipe 51 and is fed into separator 52.
  • Pipe 53 carries zinc oxide and recovered zinc soap to feed 5, from where it goes to reactor 2.
  • the liquid product goes to the three-way valve 55 through pipe 54. From the three-way valve 55 the flow is split, preferably in a differential way according to the products intended to be obtained, in flows 56 and 57. Flow 57 goes to tank 61, where biolubricants, the main product, are output.
  • Pipe 56 feeds tank 58, from which purified esters are output through pipe 59 and feed reactor 60, where hydrogen is fed from pipe 63. So, an optional hydrogenation step of one part of the esters obtained from the mixture of fatty acids with monoalcohols and polyalcohols is envisaged, increasing the degree of saturation of the esters produced.
  • the flow rates of pipes 56 and 57 can be adjusted, one with respect to the other, as needed.
  • Ratio by weight within reactor 60 is: esters:catalyst [preferably Pd (2%), SiO 2 , Al 2 O 3 ] ranging between 100:0.01 and 100:1, preferably between 100:0.1 and 100:0.5. Partial pressure of hydrogen ranges between 2 and 10 bar, preferably between 3 and 7 bar, most preferably being 5 bar.
  • Reaction temperature ranges between 90 and 180°C, preferably between 100 and 150°C, most preferably being 130°C.
  • Reaction time ranges between 10 minutes and 2 hours, preferably between 15 minutes and 1 hour.
  • Pipe 64 discharges the final product, consisting of biolubricants and, sometimes, solvents. The product discharged from pipe 64 is part of the main product too. That is, the main product, with the highest value added, is output from pipes 62 and 64.
  • the present invention allows to obtain products with high added value, from some food and lubrication wastes, which can be used in the industry as solvents or for the production of lubricants.
  • the present invention allows to recover products with high added value, completely eliminating the need of disposal treatments for some wastes.
  • disposal of products of used mineral oils treated with strong bases would be problematic, given the strongly polluting nature of these substances. For this reason, the present invention is particularly advantageous.
  • distillation and/or desorption steps can be envisaged for the purification of products of one or more steps that constitute the process, so obtaining more valuable products.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Combustion & Propulsion (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Microbiology (AREA)
  • Fats And Perfumes (AREA)

Claims (17)

  1. Verfahren für die Herstellung von Bioschmierölen, ausgehend von Seifen, verwendeten Speiseölen (UCO), tierischen Fetten, raffinierten verwendeten Speiseölen (RUCO), verwendeten Bioschmiermitteln, wobei ein Seifenansäuerungsschritt und ein Hydrolyseschritt des anderen zu regenerierenden Abfalls bereitgestellt sind, um Fettsäuren zu erhalten, dadurch gekennzeichnet, dass die Produkte dieser zwei Schritte dann mit Monoalkoholen und Polyalkoholen umgesetzt werden, um sie zu verestern, um Bioschmieröle und Lösungsmittel zu erhalten, und dass die Reaktionsprodukte verwendeter Mineralöle mit einer starken Base unter diesen Seifen eingeschlossen sind.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass besagter Hydrolyseschritt mit einem Öle/Wasser7Katalysator-Gewichtsverhältnis zwischen 100:40:1 und 200:50:5 stattfindet.
  3. Verfahren nach Anspruch 2, dadurch gekennzeichnet, dass besagtes Verhältnis 150:45:3 ist.
  4. Verfahren nach einem der vorangehenden Ansprüche, dadurch gekennzeichnet, dass in dem Hydrolyseschritt die Temperatur von einem Minimum von 170 °C bis zu einem Maximum von 250 °C reicht.
  5. Verfahren nach Anspruch 4, dadurch gekennzeichnet, dass die Temperatur von 200-210 °C reicht.
  6. Verfahren nach einem der vorangehenden Ansprüche, dadurch gekennzeichnet, dass in dem Hydrolyseschritt bei einem Druck gearbeitet wird, der zwischen 10 und 30 bar umfasst ist.
  7. Verfahren nach Anspruch 6, dadurch gekennzeichnet, dass er bei einem Druck zwischen 13 und 20 bar betrieben wird.
  8. Verfahren nach einem der vorangehenden Ansprüche, dadurch gekennzeichnet, dass während des Seifenansäuerungsschritts eine Schwefelsäure/Seifenmischung zugeführt wird, mit einem Gewichtsverhältnis im Bereich von 1:3 bis 3:1.
  9. Verfahren nach Anspruch 8, dadurch gekennzeichnet, dass ein solches Verhältnis 2:1 ist.
  10. Verfahren nach Anspruch 8 oder 9, dadurch gekennzeichnet, dass als eine Schwefelsäure eine wässrige Lösung mit einer Konzentration von 70g/l verwendet wird.
  11. Verfahren nach einem der vorangehenden Ansprüche, dadurch gekennzeichnet, dass die Ansäuerungsreaktion unter einer inerten Atmosphäre durchgeführt wird.
  12. Verfahren nach einem der vorangehenden Ansprüche, dadurch gekennzeichnet, dass der Mischungsschritt mit Monoalkoholen und Polyalkoholen mit Fettsäuren/Alkohol/Katalysator-Gewichtsverhältnissen von 100:5:1 bis 100:30:5 stattfindet.
  13. Verfahren nach Anspruch 12, dadurch gekennzeichnet, dass besagte Verhältnisse von 100:10:1 bis 100:20:3 reichen.
  14. Verfahren nach einem der vorangehenden Ansprüche, dadurch gekennzeichnet, dass während des Mischungsschritts mit Monoalkoholen und Polyalkoholen die Temperatur von 150 bis 300 °C reicht.
  15. Verfahren nach Anspruch 14, dadurch gekennzeichnet, dass während des Mischungsschritts mit Monoalkoholen und Polyalkoholen die Temperatur von 180-220 °C reicht.
  16. Verfahren nach einem der vorangehenden Ansprüche, dadurch gekennzeichnet, dass es zusätzlich einen Hydrierungsschritt eines Teils des aus dem Mischungsschritt der Fettsäuren mit Monoalkoholen und Polyalkoholen erhaltenen Ester bereitstellt.
  17. Verfahren nach einem der vorangehenden Ansprüche, dadurch gekennzeichnet, dass es einen oder mehrere Destillations- und/oder Stripping-Schritte für die Reinigung der Produkte aus einem oder mehreren Stufen, die das Verfahren ausmachen, bereitstellt.
EP22844579.7A 2021-12-30 2022-12-22 Verfahren zur herstellung von bioschmierölen Active EP4457324B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IT202100033152 2021-12-30
PCT/IB2022/062656 WO2023126789A1 (en) 2021-12-30 2022-12-22 Process for the production of lubricating biooils

Publications (3)

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EP4457324A1 EP4457324A1 (de) 2024-11-06
EP4457324C0 EP4457324C0 (de) 2026-02-04
EP4457324B1 true EP4457324B1 (de) 2026-02-04

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WO (1) WO2023126789A1 (de)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP4534635B1 (de) * 2023-10-02 2025-12-17 Itelyum Regeneration S.p.A. Verfahren zur herstellung von bioschmiermitteln aus abfallmaterialien
IT202300020376A1 (it) * 2023-10-03 2025-04-03 Itelyum Regeneration S P A Processo di produzione di biolubrificanti
EP4663724A1 (de) * 2024-06-10 2025-12-17 Itelyum Regeneration S.p.A. Verfahren zur regenerierung von fetthaltigen abfällen
EP4671350A1 (de) * 2024-06-26 2025-12-31 Itelyum Regeneration S.p.A. Verfahren zur gewinnung einer biologischen fraktion aus der regenerierung von altölen

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