Process for collecting minor components with plate short path evaporator

Abstract

The present invention relates to a process for obtaining minor components from vegetable oils, and wherein the vegetable oil includes palm oil, palm olein, palm mid-fraction or mixtures thereof. The minor components of interest are squalene, tocopherols, and optionally tocotrienols. The process is comprising, a fractionation in a plate short path evaporator. The fractionation is conducted in a plate short path evaporator with at least one evaporation section at a temperature of 140°C to 180°C, followed by at least one evaporation section at temperature of above 180°C to 240°C. The feed stream may be a condensate stream from a deodorization step.

Description

PT-2252-WO-PCTPROCESS FOR COLLECTING MINOR COMPONENTS WITH PLATE SHORT PATH EVAPORATORCROSS-REFERENCE TO RELATED APPLICATIONS

[0001] This application claims the benefit of European Application No.24213751.1, filed November 18, 2024, which is incorporated by reference herein in its entirety.FIELD OF THE INVENTION

[0002] The present invention relates to a process for obtaining minor components from vegetable oils. The minor components of interest are squalene, tocopherols, and optionally tocotri enols.BACKGROUND OF THE INVENTION

[0003] Squalene is a widely distributed natural triterpene, and it is a minor component of high commercial value worldwide because it has nutritional, pharmaceutical, medicinal, and cosmetic applications, due to its different biological properties. The main source of extraction has been shark liver oil. Secondary sources are mainly vegetable oils, although a limited one, as they allow low productive yields. Due to the diversity of applications that squalene presents and its growing demand, there is an increasing interest in identifying sustainable sources of extraction and obtaining a certain concentration / purity.

[0004] Tocopherols and tocotrienols are both part of the vitamin E family and a have a wide range of beneficial applications. Tire most common application is the use for their anti- oxidative properties.

[0005] Squalene, tocopherols and / or tocotrienol s are present in a variety of vegetable oils. Isolation of minor components from various vegetable oils and by-products of refining of vegetable oils is less efficient as minor components are present in low concentrations. There are several processes available to concentrate and purify these minor components, but they involve solvents and / or chemicals, or chromatographic separation methods.

[0006] There is a need for a suitable, more sustainable process to isolate these minor components in higher purity and / or yield, higher quality; for a simple process, preferably without involving solvents and / or chemicals.PT-2252-WO-PCT

[0007] The present invention provides for such a process.SUMMARY OF THE INVENTION

[0008] The present invention relates to a process for obtaining minor components from vegetable oils, the process is comprising:a) Fractionation of a feed stream into a distillate and a residue and the fractionation is taking place in a plate short path evaporator with at least one evaporation section at a temperature of 140°C to 180°C and at a pressure below 1 mbar;b) Collecting the distillate and / or the residue; andWherein the feed stream of step a) is comprising triglycerides, diglycerides, monoglycerides, free fatty acids, tocopherols, squalene, and optionally tocotrienols; andWherein free fatty acids are present in the feed stream in an amount of 5 to 65 wt.%; tocopherols are present in the feed stream in an amount of 0.1 to 5.0 wt.% of the feed stream, and squalene is present in an amount of 0.1 to 4.0 wt.% of the feed stream; and whereinthe vegetable oil includes palm oil, palm olein, palm mid-fraction or mixtures thereof.DETAILED DESCRIPTION

[0009] The present invention relates to a process for obtaining minor components from vegetable oils, the process is comprising:a) Fractionation of a feed stream into a distillate and a residue and the fractionation is taking place in a plate short path evaporator with at least one evaporation section at a temperature of 140°C to 180°C and at a pressure below 1 mbar;b) Collecting the distillate and / or the residue; andWherein the feed stream of step a) is comprising triglycerides, diglycerides, monoglycerides, free fatty acids, tocopherols, squalene, and optionally tocotrienols; andWherein free fatty acids are present in the feed stream in an amount of 5 to 65 wt.%; tocopherols are present in the feed stream in an amount of 0.1 to 5.0 wt.% of the feed stream, and squalene is present in an amount of 0.1 to 4.0 wt.% of the feed stream; and whereinPT-2252-WO-PCTthe vegetable oil includes palm oil, palm olein, palm mid-fraction or mixtures thereof.Vegetable Oils

[0010] The primary components of most unrefined vegetable oils are comprising triglycerides (TAG), diglycerides (DAG), monoglycerides (MAG), free fatty acids (FFA), minor components and the like.

[0011] In the present invention, the vegetable oil includes palm oil. palm olein, palm midfraction or mixtures thereof.

[0012] Unrefined vegetable oils often contain varying amounts of other components (beyond the triglycerides, diglycerides, monoglycerides), too. Some of these components are desirable components of the oil. e g., squalene, tocopherols, and / or tocotrienols, phytosterols (free and estenfied), and the like.

[0013] Vegetable oil impurities (including free fatty acids) are typically removed in the refining process, in different steps, particularly degumming, alkali treatment, bleaching, and / or deodorization.

[0014] In the deodorization step, remaining volatile impurities are removed to yield a deodorized vegetable oil having the desired final characteristics. The volatile impurities removed in the deodorization process commonly include free fatty acids (FFA), aldehydes, ketones, alcohols, and other hydrocarbon impurities.

[0015] Deodorization is typically carried out at elevated temperatures and reduced pressure to better volatilize the FFAs and other impurities. The precise temperature and pressure may vary depending on the nature and quality of the oil being processed. The pressure, for instance, will preferably be no greater than 10 mbar but in certain occasions may benefit from a pressure below or equal to 5 mbar. e.g. 1 to 3 mbar. The temperature in the deodorizer may be varied as desired to optimize the yield and quality of the deodorized oil. At higher temperatures, reactions which may degrade the quality' of the oil will proceed more quickly. For example, at higher temperatures, cis- fatty acids may be converted into their less desirable transform. Operating the deodorizer at lower temperatures may minimize the cis-to-trans conversion but will generally take longer or require more stripping medium or lower pressure to remove the requisite percentage of volatile impurities. As such, deodorization is typically performed at a temperature of the oil inPT-2252-WO-PCTa range of 180 to 270°C. with temperatures of about 220-260°C being useful for many oils. For cocoa butter-based oil, a deodorization temperature in a range of 130 to 220°C is advised.

[0016] Typically, deodorization is thus occurring in a deodorizer whereby volatile components such as FFAs and other unwanted volatile components that may cause off-flavors in the oil, are removed.

[0017] Deodorization may also result in the thermal degradation of components.

[0018] Unfortunately, some of the desirable components such as the minor components of the vegetable oil may be driven off with the volatile impurities during the deodorization process.

[0019] As a consequence, the volatile stream exiting the deodorizer will include a substantial fraction but may also include a varying amount of desirable components.Minor Components

[0020] In an aspect of the invention, the minor components are tocopherols, tocotrienols, triterpenes (such as squalene, alfa-amyrin, beta-amyrin and the like), phytosterols (free sterols and sterol esters).

[0021] In an aspect of the invention, the minor components are squalene, tocopherols, tocotrienols and phytosterols.

[0022] In a further aspect of the invention, the minor components are squalene, tocopherols and tocotrienols.

[0023] In another aspect of the invention, the minor components are squalene and tocopherols.Feed Stream

[0024] Feed stream is the starting material used for the fractionation.

[0025] The feed stream is comprising triglycerides, diglycerides, monoglycerides, free fatty acids, tocopherols, squalene, and optionally tocotrienols and; and wherein free fatty acids are present in the feed stream in an amount of 5 to 65 wt.%; tocopherols are present in the feed stream in an amount of 0.1 to 5.0 wt.% of the feed stream, and squalene is present in an amount of 0.1 to 4.0 wt.% of the feed stream.

[0026] In an aspect of the invention, the feed stream is comprising tocopherols in an amount of 0.1 to 3.0 wt.% of the feed stream.PT-2252-WO-PCT

[0027] In an aspect of the invention, the feed stream is comprising squalene in an amount of 0.1 to 2.0 wt.% of the feed stream.

[0028] In an aspect of the invention, the feed stream is comprising phytosterols in an amount of 0.7 to 6.0 wt.% of the feed stream.

[0029] In an aspect of the invention, the feed stream is comprising triglycerides in an amount of 7 to 55 wt.% based on weight of the feed stream.

[0030] In an aspect of the invention, the feed stream is comprising diglycerides in an amount of 15 to 35 wt.% based on weight of the feed stream.

[0031] In an aspect of the invention, the feed stream is comprising monoglycerides in an amount of 1 to 4.5 wt.% based on weight of the feed stream.

[0032] In an aspect of the invention, the feed stream is comprising tocotrienols in an amount of 0.1 to 2 wt.% of the feed stream.

[0033] In an aspect of the invention, the feed stream is sourced from vegetable oils that include palm oil or palm oil fractions, sunflower oil, rapeseed oil, soybean oil, rice bran oil, palm kernel oil, coconut oil, shea butter or mixtures thereof.

[0034] In an aspect of the invention, the feed stream is sourced from vegetable oil including palm oil, palm olein, palm mid-fraction or mixtures thereof.

[0035] In an aspect of the invention, the feed stream is a condensate stream of a deodorization step of a vegetable oil.

[0036] A deodorization step of a vegetable oil can be conducted such that a deodorized vegetable oil and a volatiles stream is obtained. A condensation stream can be obtained by partial and / or complete condensation of the volatiles stream. The condensation stream is cooled at a certain temperature, here referred to as the condenser temperature. The condensation stream comprises a portion of the glycerides and a majority of the volatile impurity fraction of the vegetable oil, as well as the minor components of interest. Such a condensate stream may be the feed stream of the present invention.

[0037] In an aspect of the invention, the condensate stream is obtained at a condenser temperature of from 100°C to 180°C, preferably from 140°C to 160°C.

[0038] In an aspect of the invention, the feed stream, preferably a condensate stream is comprising:- triglycerides in an amount of 7 to 55 wt.%, preferably from 20 to 40 wt.% based on weight of the feed stream,PT-2252-WO-PCT- diglycerides in an amount of 15 to 35 wt. %. preferably from 20 to 32 wt. % based on weight of the feed stream,- monoglycerides in an amount of 1 to 4.5 wt.% preferably from 2.0 to 4.0 wt.% based on weight of the feed stream,- free fatty acids in an amount of 5 to 65 wt. % based on weight of the feed stream; preferably from 15 to 35 wt.% based on weight of the feed stream,- tocopherols in an amount of 0.1 to 5.0 wt.% based on weight of the feed stream, preferably from 0.1 to 3.0 wt.% based on weight of the feed stream,- squalene in an amount of 0.1 to 4.0 wt.% based on weight of the feed stream, preferably from 0.1 to 2.0 wt.% based on weight of the feed stream; and

[0039] In an aspect of the invention, the vegetable oils are selected from palm oil, palm olein, palm mid-fraction or mixtures thereof, and the feed stream, preferably a condensate stream is comprising:- triglycerides in an amount of 7 to 55 wt.%, preferably from 20 to 40 wt.% based on weight of the feed stream,diglycerides in an amount of 15 to 35 wt. %, preferably from 20 to 32 wt. % based on weight of the feed stream,- monoglycerides in an amount of 1 to 4.5 wt.% preferably from 2.4 to 4.0 wt.% based on weight of the feed stream,free fatty acids in an amount of 5 to 65 wt. % based on w eight of the feed stream; preferably from 15 to 35 wt.% based on weight of the feed stream,- tocopherols and tocotrienols in an amount of 0.1 to 3.0 wt.% based on weight of the feed stream;squalene in an amount of 0.1 to 2.0 wt.% based on weight of the feed stream; and

[0040] In an aspect of the invention, the enzymatic treated feed stream is comprising phytosterols in an amount of 0.7 to 6.0 wt.% of the feed stream.Fractionation

[0041] The feed stream is fractionated in a plate short path evaporator.PT-2252-WO-PCT

[0042] In an aspect of the invention, the fractionation of step b) is conducted in a plate short path evaporator with at least one evaporation section at a temperature of 140°C to 180°C, followed by at least one evaporation section at temperature of above 180°C to 240°C.

[0043] In an aspect of the invention, the fractionation of step b) is conducted in a plate short path evaporator with at least one evaporation section at a temperature of 140°C to 180°C follow ed by at least one evaporation section preferably at a temperature of from 190°C to 230°C, more preferably at a temperature of from 200°C to 220°C or from 210°C to 215°C.

[0044] A plate short path evaporator that can be used in the present invention is described in WO 2010 / 034043 or in pending application PCT / US2024 / 030173.

[0045] A suitable plate short path evaporator is having multiple evaporation sections, configured to comprising more than one heatable evaporator plate extending vertically in the housing, and more than one condensation section associated with the evaporation sections, and the evaporation sections and the condensation sections are arranged in an alternating order, with an evaporation section being alternated with a condensation section.

[0046] The plate short path evaporator applied in the present invention allows for conducting a process with multiple temperature ranges. The multiple temperature ranges can be achieved in the different sections available in one and the same equipment (plate short path evaporator). In comparison with standard short evaporator, either multiple equipment and / or multiple passes are needed, while in the present invention with the use of the plate short path evaporator having multiple evaporation stages in one equipment, there is no need for more than one equipment and / or multiple passes in the same equipment.

[0047] The evaporation in plate short-path evaporator used in step a) of the process according to the invention is performed at a pressure below 1 mbar, preferably below 0.1 mbar, more preferably below 0.01 mbar, most preferably below' 0.005 mbar.

[0048] The evaporation in plate short-path evaporator is further performed at specific conditions of temperature and feed rate per unit area of evaporator surface of the plate shorth-path evaporation equipment. The plate short path evaporator allows for having bigger surface areas than a common short evaporator.

[0049] The “feed rate per unit area of evaporator surface of the plate shorth-path evaporation equipment"’, also called “specific throughput"’ or “specific feed rate”, expressed in kg / h per m2. is defined as the flow of oil, expressed in kg / h, per unit area of evaporator surface of the plate short-path evaporation equipment, expressed in m2PT-2252-WO-PCT

[0050] In an aspect of the invention, the short path evaporator is operated with a feed rate (flow rate) (kilogram per hour) per unit area of evaporator surface of the shorth-path evaporation equipment in a range of from 10 to 200 kilogram per hour per square meter (kg / h per m2), preferably from 12 to 150 kilogram per hour per square meter (kg / h per m2), more preferably in a range of from 15 to 100 kilogram per hour per square meter (kg / h per m2), even more preferably in a range of from 17 to 80 kilogram per hour per square meter (kg / h per m2), most preferably in a range of from 20 to 50 kilogram per hour per square meter (kg / h per m2)

[0051] The fractionation of the feed stream provides a distillate and a residue.

[0052] In an aspect of the invention, the distillate collected in step b) is comprising i. Tocopherols in an amount of up to 7 wt.% based on weight of the distillate; and ii. Squalene in an amount of 1 to 5 wt.% based on weight of the distillate

[0053] In an aspect of the invention, the distillate is comprising phytosterols in an amount of 3 to 10 wt.% based on weight of the distillate.

[0054] In an aspect of the invention, the distillate collected in step b) is further comprising i. Triglycerides in an amount of less than 5 wt.% based upon the weight of the distillate;ii. Diglycerides in an amount of 0.5 to 4 wt.% based on weight of the distillate; iii. Free fatty acids in an amount of 65 to 95 wt.% based on weight of the distillate;iv. Monoglycerides in an amount of 3 to 15 wt.% based on weight of the distillate:

[0055] In an aspect of the invention, the distillate collected in step b) is comprising i. Triglycerides in an amount of less than 5 wt.% based upon the weight of the distillate;ii. Diglycerides in an amount of 0.5 to 4 wt.% based on weight of the distillate; iii. Free fatty acids in an amount of 65 to 95 wt.% based on weight of the distillate;iv. Monoglycerides in an amount of 3 to 15 wt.% based on weight of the distillate:PT-2252-WO-PCTv. Tocopherols in an amount of up to 7 wt.% based on weight of the distillate;andvi. Squalene in an amount of 1 to 5 wt.% based on weight of the distillate.

[0056] In an aspect of the invention, the vegetable oils are selected from palm oil, palm olein, palm mid-fraction or mixtures thereof and the distillate collected in step b) is comprising:iii. Tocopherols and tocotrienols in an amount of up to 7 wt.% based on weight of the distillate;iv. Squalene in an amount of 1 to 5 wt.% based on weight of the distillate;

[0057] In an aspect of the invention, the vegetable oils are selected from palm oil, palm olein, palm mid-fraction or mixtures thereof and the distillate collected in step b) is further comprising:i. Triglycerides in an amount of less than 5 wt.% based upon the weight of the distillate;ii. Free fatty7acids in an amount of 65 to 95 wt.% based on weight of the distillate.

[0058] In an aspect of the invention, the vegetable oils are selected from palm oil, palm olein, palm mid-fraction or mixtures thereof and the distillate collected in step b) is comprising:i. Triglycerides in an amount of less than 5 wt.% based upon the weight of the distillate;ii. Diglycerides in an amount of 0.5 to 4 wt.% based on weight of the distillate; iii. Monoglycerides in an amount of 3 to 15 wt.% based on weight of the distillate;iv. Free fatty acids in an amount of 65 to 95 wt.% based on weight of the distillate;v. Tocopherols and tocotrienols in an amount of up to 7 wt.% based on weight of the distillate;vi. Squalene in an amount of 1 to 5 wt.% based on weight of the distillate.

[0059] In an aspect of the invention, the residue is collected.PT-2252-WO-PCT

[0060] In an aspect of the invention, the residue collected in step b) is comprisingi. Triglycerides in an amount of 30 to 45 wt.% based upon the weight of the residue;ii. Diglycerides in an amount of 30 to 45 wt.% based on weight of the residue.

[0061] In an aspect of the invention, the vegetable oils are selected from palm oil, palm olein, palm mid-fraction or mixtures thereof and the residue collected in step b) is comprising i. Tocopherols and tocotrienols in an amount of 1 to 5 wt.% based on weight of the residue;ii. Squalene in an amount of 0.1 to 1.5 wt.% based on weight of the residue.

[0062] In an aspect of the invention, the vegetable oils are selected from palm oil, palm olein, palm mid-fraction or mixtures thereof and the residue collected in step b) is further comprisingi. Triglycerides in an amount of 30 to 45 wt.% based upon the weight of the residue;ii. Diglycerides in an amount of 30 to 45 wt.% based on weight of the residue.

[0063] In an aspect of the invention, it relates to a process for obtaining minor components from vegetable oils, and the process is comprising:a) Fractionation of the feed stream into a distillate and a residue and the fractionation is taking place in a plate short path evaporator with at least one evaporation section at a temperature of 140°C to 180°C, followed by at least one evaporation section at temperature of above 180°C to 240°C;b) Collecting the distillate and / or collecting the residue; andWherein the feed stream of step a) is comprising triglycerides, diglycerides, monoglycerides, free fatty acids, tocopherols, squalene and optionally tocotrienols; andWherein free fatty acids are present in the feed stream in an amount of 5 to 65 wt.%; tocopherols are present in the feed stream in an amount of 0.1 to 5.0 wt.% of the feed stream, and squalene is present in an amount of 0.1 to 4.0 wt.% of the feed stream.PT-2252-WO-PCT

[0064] In an aspect of the invention, it relates to a process for obtaining minor components from vegetable oils, and the process is comprising:a) Fractionation of the feed stream into a distillate and a residue and the fractionation is taking place in a plate short path evaporator with at least one evaporation section at a temperature of 140°C to 180°C, followed by at least one evaporation section at temperature of above 180°C to 240°C;b) Collecting the distillate and / or collecting the residue; andWherein the feed stream of step a) is comprising triglycerides, diglycerides, monoglycerides, free fatty acids, tocopherols, squalene and optionally tocotrienols; andWherein free fatty acids are present in the feed stream in an amount of 5 to 65 wt.%; tocopherols are present in the feed stream in an amount of 0.1 to 3.0 wt.% of the feed stream, and squalene is present in an amount of 0.1 to 2.0 wt.% of the feed stream.

[0065] In an aspect of the invention, it relates to a process for obtaining minor components from vegetable oils selected from palm oil, palm olein, palm mid-fraction or mixtures thereof, and the process is comprising:a) Fractionation of the feed stream into a distillate and a residue and the fractionation is taking place in a plate short path evaporator with at least one evaporation section at a temperature of 140°C to 180°C, followed by at least one evaporation section at temperature of above 180°C to 240°C;b) Collecting the distillate and / or collecting the residue; andWherein the feed stream of step a) is comprising triglycerides, diglycerides, monoglycerides, free fatty acids, squalene, tocopherols and tocotrienols; and Wherein free fatty acids are present in the feed stream in an amount of 5 to 65 wt.% tocopherols and tocotrienols are present in the feed stream in an amount of 0.1 to 3.0 wt.% of the feed stream, and squalene is present in an amount of 0.1 to 2.0 wt.% of the feed stream.

[0066] The advantages of the present invention are amongst others:PT-2252-WO-PCT- Isolation of minor components from various streams is difficult as they are present in low concentrations; but the process of the present invention allows the concentration of the minor components without using solvents and / or chromatographic separation methods; - Avoiding long heat treatments and thus reduce breakdown of the heat-sensitive minor components;- Provision of distillates with high value due to the high amount of minor components, that can have multiple applications;- Pre-enriches minor components, which helps further process capabilities to operate at higher throughput / higher capacity;- Use of plate short path evaporator allows a smooth / mild process, and multiple temperature ranges can be applied in one equipment;- There is no need for a multiple pass or multiple standard short path evaporators (commonly- used) to obtain the same yield and purity of the minor components;- Plate short path evaporator has multiple sections allowing for different temperature ranges which cannot be achieved with the standard short path evaporator;- A single pass over a plate short path evaporator is providing similar results as a double pass over a standard short path evaporator (commonly used);- Plate short path evaporator has a bigger surface area than a "common" short path evaporator (standard short path evaporator);- A more sustainable process, due to lower energy consumption;- A more sustainable process, due to reduced CO2emission;- The residue can be re-cycled back into the overall process of deodorization of vegetable oilConducting the fractionation first at a temperature of 140°C to 180°C and at a pressure below 1 mbar allows retaining the minor components and is avoiding losses that take place when the initial fractionation is taking place at higher temperature;- Tocopherols and squalene are enriched and are collected in one vessel

Claims

PT-2252-WO-PCTCLAIMS1. A process for obtaining minor components from vegetable oils, the process is comprising:a) Fractionation of the feed stream into a distillate and a residue and the fractionation is taking place in a plate short path evaporator with at least one evaporation section at a temperature of 140°C to 180°C and at a pressure below 1 mbar;b) Collecting the distillate and / or the residue; andWherein the feed stream of step a) is comprising triglycerides, diglycerides, monoglycerides, free fatty acids, tocopherols, squalene, and optionally tocotrienols; andWherein free fatty acids are present in the feed stream in an amount of 5 to 65 wt.%; tocopherols are present in the feed stream in an amount of 0.1 to 5.0 wt.% of the feed stream, and squalene is present in an amount of 0.1 to 4.0 wt.% of the feed stream; and whereinthe vegetable oil includes palm oil, palm olein, palm mid-fraction or mixtures thereof.

2. The process according to claim 1 wherein the feed stream is comprising:a) Triglycerides in an amount of 7 to 55 wt.% based on weight of the feed stream.

3. The process according to claim 1 or 2 wherein the feed stream is comprising:a) Diglycerides in an amount of 15 to 35 wt.% based on weight of the feed stream; b) Monoglycerides in an amount of 1 to 4.5 wt.% based on weight of the feed stream.

4. The process according to anyone of the preceding claims wherein the fractionation of step b) is conducted in a plate short path evaporator having multiple evaporation sections and with at least one evaporation section at a temperature of 140°C to 180°C, followed by at least one evaporation section at temperature of above 180°C to 240°C.

5. The process according to anyone of the preceding claims wherein the distillate of step b) is comprisinga) Tocopherols, and optionally tocotrienols in an amount of up to 7 wt.% based on weight of the distillate; andPT-2252-WO-PCTb) Squalene in an amount of 1 to 5 wt.% based on weight of the distillate6. The process according to anyone of the preceding claims wherein the distillate of step b) is comprisingi. Triglycerides in an amount of less than 5 wt.% based upon the weight of the distillate;ii. Diglycerides in an amount of 0.5 to 4 wt.% based on weight of the distillate; iii. Free fatty acids in an amount of 65 to 95 wt.% based on weight of the distillate; iv. Monoglycerides in an amount of 3 to 15 wt. % based on weight of the distillate;7. The process according anyone of the preceding claims wherein the residue of step b) is comprisingi. Triglycerides in an amount of 30 to 45 wt.% based upon the weight of the residue;ii. Diglycerides in an amount of 30 to 45 wt.% based on weight of the residue.

8. The process according to any one of the preceding claims wherein the feed stream is a condensate stream of a deodorization step of a vegetable oil.

9. The process according to claim 13 wherein the condensate stream is obtained at a condenser temperature of from 100°C to 200°C.

10. The process according to anyone of the preceding claims wherein the process is comprising the following steps:a) Fractionation of the feed stream into a distillate and a residue and the fractionation is taking place in a plate short path evaporator having multiple evaporation sections and with an evaporation section at a temperature of 140°C to 180°C, followed by an evaporation section at temperature of above 180°C to 240°C;b) Collecting the distillate and / or the residue; andWherein the feed stream of step a) is comprising triglycerides, diglycerides, monoglycerides, free fatty acids, tocopherols, squalene and optionally tocotrienols; andPT-2252-WO-PCTWherein free fatty acids are present in the feed stream in an amount of 5 to 65 wt.%; tocopherols are present in the feed stream in an amount of 0.1 to 3.0 wt.% of the feed stream, and squalene is present in an amount of 0.1 to 2.0 wt.% of the feed stream and whereinthe vegetable oil includes palm oil, palm olein, palm mid-fraction or mixtures thereof.