TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Method: Short-chain (up to 4C atoms aliphatic alcohols) is used. The transesterification reaction is carried out at molar proportion of fatty raw material calculated to triglycerides and alcohol of greater than or equal to1:10, preferably 1:18. Alcoholic solution of catalyst agent of several-mole concentration is prepared directly by dissolving hydroxide metal, e.g. potassium hydroxide (KOH), in anhydrous aliphatic alcohol, e.g. ethanol, at increased temperature. Distillation off is carried in two stages: first at lower temperature (up to 353degreesK) under 0.25 atm, then at up to 370degreesK, to remove 1.5 wt.% of azeotropic fraction. For separation of ester phase, there is applied separation of the mixture to upper ester phase and lower glycerine phase, which separates very slowly after sedimentation and remove from the process; and the remaining ester phase is centrifuged and filtrated in hydrophilic conditions at lower pressure, then there is used a known bleaching method. In the case of solid fat, it is warmed up to melting, that is up to greater than or equal to318degreesK and, in addition, the solid fraction is centrifuged from the ester phase at 40 wt.%, and then it is integrated with liquid phase. Vegetable fats, preferably rape-seed oil coldly pressed, and animal origin fats are used as fatty raw materials. EXAMPLE - 3000 g Crude rape oil coldly pressed was put into a reactor, and then the space over the liquid surface was filled with dry nitrogen under 1010 hPa. Then 2710 g of anhydrous ethyl alcohol (99.8% bioethanol) was introduced into the reactor during continuous stirring, then there was added the catalyst solution prepared by dissolution of 29.4 g potassium hydroxide of technical degree in 100 g anhydrous ethyl alcohol in the atmosphere of dry nitrogen. Molar proportion of rape oil (calculated to triglycerides) to anhydrous ethyl alcohol was 1:18. The reactor content was stirred intensively for 20 minutes, maintaining temperature of 298degreesK, and just after 3 minutes there was observed homogenization of the mixture, which manifested in complete transparency of the mixture in the reactor. The post-reaction mixture was transferred into a vacuum evaporator, previously washed out with dry nitrogen and equipped with a low-temperature trap cooled with vapors of liquid nitrogen. The trap minimized ethyl alcohol losses during process of distillation off of alcohol excess from the reaction mixture. The process of distillation off was carried out for 15 minutes in a bath 333degreesK and under 250 hPa. After the increase of the bath temperature up to 358degreesK, the small amount (up to 1.5%) of azeotropic fraction was distilled off. In this way, the alcohol was practically completely removed from the reaction space. The mixture remaining in the vacuum evaporator was transferred immediately into a pear-shaped distributor of volume of 4 dm3. After a few minutes there was observed phase separation of the warm mixture in the bottom glycerine phase and upper-ester one. After 6 hours the glycerine phase was very slowly let out into a separate container, while the ester phase was separated again and put through a filter of strong hydrophilic properties, using a set for filtration under lower pressure. Such purified ester undergone bleaching process in nitrogen atmosphere. 3000 g Ethyl ester of the long-chain fatty acids, of pale straw color, was obtained.