AU2012203418A1 - Integrated process for the production of biofuels from different types of starting materials and related products - Google Patents

Abstract

Process for the production of biocombustible or biofuel mixtures suitable for different conditions of use, starting from refined or raw vegetable oils, including those extracted from seaweed, and/or from used food oils and animal fats, each of which is pre-treated with specific treatments in order to yield a dried refined oil. The latter then undergoes transesterification with an excess of lower alcohols or bioalcohols, and a subsequent separation into a raw glycerine-based phase and a phase containing mixtures of fatty acid alkyl esters and the excess alcohols or bioalcohols.; The excess amount of lower alcohols/bioalcohols can be partially or completely recovered from the obtained mixture, or the mixture itself may be integrated with additional quantities of the same or different lower alcohols/bioalcohols, thereby yielding combustible products and ecological fuels suitable for various environmental conditions and 'for the types of apparatus and engines they must be employed in. The product can either be used by itself or as the main or secondary ingredient of a mixture with conventional fuel.

Description

1 AUSTRALIA Patents Act 1990 NAZZARENO DE ANGELIS COMPLETE SPECIFICATION STANDARD PATENT Invention Title: Integrated process for the production of biofuels from different types of starting materials and related products The following statement is a full description of this invention including the best method of performing it known to us:- 1A INTEGRATED PROCESS FOR THE PRODUCTION OF BIOFUELS FROM DIFFERENT TYPES OF STARTING MATERIALS AND RELATED PRODUCTS 5 The present invention concerns an integrated process for the produc tion of biofuels and biocombustibles from different types of starting materials and the related products. More specifically, the intention concerns a process yielding new biofuel mixtures from the treatment of refined or raw vegetable 10 oils, including those extracted from algae and/or microalgae, either seaweed or other varieties, produced in aquaculture or in thermal bioreactors, and from the treatment of animal fats and used frying oils, as well as through feeding calibrated proportions of alcohols or bioalcohols of low molecular weight into the oil-based mixture in order to obtain combustible products and ecological 15 fuels suitable for the various environmental conditions and for the kinds of systems or engines they must be used in. As is known, the demand for renewable, ecologically compatible en ergy is increasingly more pressing in view of the gradual reduction of fossil fuel reserves and of the environmental risks represented by increasing atmos 20 pheric pollution and the greenhouse effect. This it why the study and devel opment of fuels and combustibles of biological 'origin has considerably in creased over the last few decades.'Two of the most widespread and consoli dated methods for producing energy starting from biomass are bioethanol and biodiesel production. 25 In general, biomass means any organic substance or material directly or indirectly deriving from chlorophyll photosynthesis. Through this process, plants take in water and carbon dioxide from their environment .and, through the sun's energy and the nutrients present in the soil, the water and carbon dioxide are then turned into organic material useful for the plant's growth. 30 From a production standpoint, the most important types of biomass are for estry residues, waste products from the timber and papermaking industry, waste of zootechnics enterprises and municipal solid waste, but also vegeta- -2 ble materials coming from specific cultivations such as sugar beet and sugar cane, cereals and their waste products, algae and/or microalgae, aquaculture and/or in thermal bioreactors, and oleaginous seeds of plants such as soy, colza and sunflower. It is evident that, if the materials produced either directly 5 or indirectly from these agricultural activities are used for energy applications involving combustion, then, on the one hand, the energy generated will not affect fossil fuel reserves and, on the other, the carbon dioxide produced in this combustion will be compensated, in the overall energy balance, by the carbon dioxide consumed by the relative plant of origin via the chlorophyll 10 synthesis. Bioethanol is produced by the anaerobic fermentation of biomasses containing sugars and/or starches, such as various cereals and their waste products, various wastes of agrofood processing and cultivations, and sugar cane and sugar beet production. Specifically, sugarcane is grown deliberately 15 for the production of bioethanol for motor vehicles. This is particularly found in Brazil, where ethyl alcohol is the main source of fuel commonly used in inter nal combustion engines. Also in Europe, bioethanol has been taken into-con sideration as a possible petrol substitute, even if its energy yield is lower than that of petrol and a complete substitution would call for the use of specially 20 designed engines. According to current European Union legislation, bioetha nol must be used in an amount of 1% in a mixture with petrol. This percentage is destined to rise to 5% and requires making no changes to existing engines. Moreover, in some countries like France and Spain, ethyl tertiary buthyl ether (ETBE), a tertiary butyl ether derived from bioethanol, is currently used in a 25 15% mix with petrol. Finally, in northern European countries like Sweden there are already newly designed cars circulating that are fuelled by an 85% bio ethanol and 15% petrol mixture. Biodiesel is instead meant to replace diesel fuel in motor vehicles and heating systems, and is obtained from widespread purposely grown oleagi 30 nous plants like colza and sunflower. Other starting materials include soy, maize, cotton, coconut, palm seed'or linseed oils or even oils deriving from marine or other algae and/or microalgae either produced in aquaculture or in -3 thermal bioreactors, or spent food oils such as used frying oils, and animal fats. The oils contained in these products (generally known as "combustible vegetable oil" or "pure vegetable oil") are triglycerides of fatty acids in which the fatty acid alcohol chains linked to the glycerine molecule normally contain 5 12-18 carbon atoms. Owing to their high viscosity, these products must be treated in order to break down the triglyceride molecules into three separate molecules, derived from fatty acids, and into a glycerine molecule. In effect, the treatment replaces the glycerine triester with three monoesters of a lower alcohol, normally methanol or ethanol, according to the following reaction, 10 where R, R' and R" represent saturated or unsaturated alcohol chains, nor mally with 12-22 carbon atoms, and, in the case shown, the alcohol replacing glycerine is methanol. 0 H 0 H H- C -- C--R H- C -OH CH 3 -0-C-R 0 0

II

H-C-0-C-R' + 3 CH 3 0H - H- C -OH + CH 3 -0-C-R' 0 H-C-O--R" H- C -OH 11

CH

3 -0-C-R" H H triglyceride 3 methanol glycerol 3 fatty acid methyl esters 15 There are three basic-ways to produce alkyl esters for biofuels starting from oils and fats of biological origin (biolipids): - direct base-catalysed transesterification of the biolipid. - direct acid-catalysed transesterification of the biolipid. - conversion of the biolipid first into fatty acids and then into lower alkyl 20 esters. Transesterification, which is practically an alcoholysis of the triglyc eride by means of a short-chain monofunctional alcohol, mainly methanol or ethanol, is the most convenient transformation method. In particular, base catalysed transesterification (with a homogeneous catalyst, that is, in solution -4 in the reaction mixture) is the cheapest and currently most widespread proc ess. It normally requires temperatures in the region of 70-130"C and pres sures of 1-1.5 bar, with a conversion yield of about 85%. The biodiesel produced by transesterification from combUstible vege 5 table oil thus consists of a mixture of alkyl esters, particularly methyl or ethyl esters, of fatty acids and has a more homogeneous overall composition than that of fossil diesel fuel; it also has greater biodegradability and greater oxy gen content because each molecule contains an ester function, -0-CO-. As will be clearer below, biodiesel use, if compared to fossil fuel use, 10 enables.a reduction in the gaseous emissions of engines that are considered dangerous for health. Moreover, as already noted, this use allows to bring to zero the balance of the carbon dioxide produced, thereby contributing to limit ing the overall greenhouse effect in the atmosphere. This is because the CO 2 produced in the combustion of a certain amount of biodiesel quantitatively 15 corresponds to the amount used in the photosynthesis in the cultures for the production of vegetable oils destined for biofuels. According to current European legislation, biodiesel' is used in amounts of 1% in a mixture with conventional diesel fuel for motor vehicles, but these amounts should shortly reach and exceed 5%. Larger amounts, 20 even 30%, are already used in certain vehicles, such as in public transport buses. In this case, too, using up to about 30% of biodiesel in diesel engines does not need any particular technical modifications, while more recently designed engines can even be fuelled by 100% pure biodiesel. The older biodiesel production plants using combustible vegetable oils 25 as starting material are besed on processes in batch. They generally use only one kind of starting material and the transesterification process takes place in a single phase. As already noted, in traditional production plants, transesterifi cation takes place at a relatively high temperature (such as 130*C) and there is a limited recovery of the catalyst, and a methanol recovery only in the final 30 phase of the process. Particular care is necessary to monitor the quantity of water and free fatty acids in the starting biolipid. If the level of free fatty acids or humidity is too high, there may be processes of saponification and glycerine -5 separation at the end of the process. With traditional processing plants, the final product obtained is a mix ture of methyl esters with a high humidity and glycerine content: the glycerine obtained as a by-product has a purity ranging between 75% and 80%. 5 Processing plants of more recent construction operate in a continuous mode and at a lower temperature (around 70 0 C), and in this case the trans esterification takes place in several stages, with recovery of both methanol and ethanol, which can be recycled in the process. To accelerate the process, besides using suitable catalysts enhancing the speed and efficiency of the 10 reaction, excess alcohol is used (normally 1:6, expressed in moles, that is, double the stoichiometric ratio) and the glycerine formed is eliminated. The alcohol in the alkyl ester solution can be separated by distillation, while a small part remains in the aqueous solution, from which it can also be extracted. 15 An example of the continuous process for producing alkyl esters (in particular, methyl esters) of fatty acids deriving from vegetable oils and using homogeneous catalysis techniques with soluble bases as catalysts, such as sodium hydroxide and sodium methylate, and in which the reaction is carried out in at least two consecutive stages, is described in European patent EP 20 0523767 (Metallgesellschaft AG). The fuel of biological origin which is currently referred to as biodiesel, which has been briefly described above, does not have suitable characteris tics for certain final uses, including use at low temperatures. This is the case, for example, with aeronautical applications, where engines must be able to 25 run at temperatures in the region of -70'C. As is known, turbine engines are used both in energy production and in the aeronautical industry. Their positive features consist of their quick start up of plants and thus the immediate availability of power, as well as good functional reliability. On the other hand, they entail considerable energy con 30 sumption and pollution, especially at maximum power levels. In the aeronauti cal case, the maximum power requirement of an aircraft is when taking off and landing, and this adds to air pollution.

-6 For their characteristics, turbine power stations should be activated only to cover peak energy consumption times and emergencies, but in coun tries where demands for energy exceeds the availability, these power stations are used for very long periods. 5 Both as regards use in aviation and in power stations, besides reduc ing fuel consumption, it would be extremely advantageous to have fuels that can reduce pollutants emissions, and this is why also in these fields the avail ability of suitable fuels or combustibles of biological origin is extremely impor tant. The possibility of diluting normal aircraft fuel with a biocompatible product 10 of a biodiesel type, but which can be calibrated to obtain the functional charac teristics suitable for use in extreme conditions as those of aircraft engines, would meet important criteria of economy and environmental protection in this field. In view of the above, an object of the present invention is to provide a 15 production process to obtain biofuel mixtures that can, on the one hand, be extremely flexible as regards supply of raw materials, being suitable to proc ess any material based on animal or vegetable oil or fat including waste mat ter of food processing and used frying oils, while, on the other hand, offering the same high flexibility as regards the characteristics of usability of the result 20 ing product. In particular, such product must be able to withstand the same conditions as any normal biodiesel, either in a pure state or diluted with estab lished amounts of fossil fuel, but it must also be available for use - in more suitable quantities and proportions of its components - as fuel or as a diluent of conventional fuels, in extreme conditions, and particularly at low tempera 25 tures, or in situations where the extreme purity of emissions is a critical re quirement. To this end, the present invention proposes a process essentially based on the transesterification of vegetable oils of various origin, both raw and refined oils, of biolipids of animal origin or even lipid-based waste prod 30 ucts of food processing, such as used frying oils. Before undergoing the transesterification process, these materials are suitably pre-treated according to the kind of starting material and its origin, and then suitably dried in order to -7 provide a dried refined oil that is as consistent and reproducible as possible for the transesterification process. Downstream of transesterification, in the process proposed according to the present invention, the lower alcohol that is used in excess for transesterification can be completely separated from the 5 reaction mixture and recovered, or it can be recovered in part, or may even be fed into the final mixture with a quantity of additional alcohol, of .the same or different type, in order to obtain - in the final product - a calibrated quantity of one or more different lower alcohols in a mixture with the fatty acid alkyl esters resulting from the transesterification process. 10 The new product resulting from the aforesaid process is synthetically called "Bio-oil" to distinguish it (both in terms of intrinsic constitution and per formance) from conventional biodiesel. Thus, the present invention specifically provides a process for the production 15 of biocombustible and biofuel mixtures suitable for different conditions of use, comprising the following fundamental operations: a) producing mixtures of fatty acid alkyl esters and glycerine by trans esterification, starting from lipid-based vegetable or animal materials and from lower alcohols or bioalcohols in excess; 20 b) separating the mixtures deriving from the said operation a) of trans esterification into a phase based on raw glycerine and a phase contain ing the said mixtures of fatty acid alkyl esters and the excess amount of lower alcohols or bioalcohols; characterised by the fact that the said starting lipid-based vegetable or animal 25 materials include one or more of the following ingredients: i. raw vegetable oil ii. refined vegetable oil iii. used food oil and/or animal fats and by the fact that the said ingredients undergo the following preliminary 30 treatments upstream of said operation a) of transesterification: 1) the said ingredient i), raw vegetable oil, is subjected to a prelimi nary depuration and refining treatment in order to remove impuri- -8 ties and to neutralise and winterize it, and then to drying of the re fined oil thus obtained; 2) the said ingredient ii), refined vegetable oil, is subjected to pre liminary drying; 5 3) the said ingredient iii), used food oil and/or animal fats, is sub jected to a preliminary depuration treatment, to drying and then to an esterification of the free fatty acids contained therein, by ad diion of lower alcohols or bioalcohols; the obtained product based on fatty acid alkyl esters is mixed in a proportion of not more than 10 20% with dried refined oil obtained from treatments 1) or 2) above. The said proportion is preferably 15%. According to the present invention, after the operation b) of separation of the reaction mixture coming from transesterification, the phase containing the mixtures of fatty acid alkyl esters and the excess amount of lower alcohols 15 or bioalcohols can be subjected to a further treatment for the separation of amounts ranging from 0 to 100%, preferably from 10 to 100%, of alcohols or bioalcohols present after operation b) of separation. In practice, the said phase may not necessarily be subjected to further separation treatments, thus keeping the whole excess quantity of lower alcohols or bioalcohols in the final 20 product. Alternatively, according to the uses envisaged for the product and to the environmental conditions of use, the phase containing the mixture of fatty acid alkyl esters and excess lower alcohols or bioalcohols may be added with a further quantity of lower alcohols or bioalcohols. 25 From the above, it results that Bio-oil is a new biofuel obtained from suitable combinations of percentages of its main components - esterified oils and alcohols/bioalcohols. It may be used alone or as the main ingredient of a mixture, or as a biocompatible diluent in variable percentages, in relation to the characteristics 30 and use of the apparatus it is used in and the relative environmental condi tions of use (such as low temperatures), be it a turbogas engine, an internal combustion engine, a fuel cell, a burner, for applications in the fields of land, sea or air transportation, mechanical or electrical energy production or heating systems. Preferably, the said lower alcohols or bioalcohols are selected from among methanol, ethanol, biomethanol, bioethanol and their mixtures, but the 5 definition of lower alcohol embraces alcohols with up to 4 carbon atoms. Preferably, the said operation a) of transesterification is carried out with an alkaline catalyst, according to what is already consolidated in biodiesel production, such as sodium or potassium hydroxide or sodium methylate. According to certain preferred embodiments of the present invention, this 10 operation is carried out in three consecutive steps in which thd said alcohols or bioalcohols and said catalyst are dosed and recycled at every passage. This operative solution is advantageous as regards yields, because it allows making the transesterification process go further. In the process according to the present invention, the transesterifica 15 tion takes place continuously, preferably at a maximum temperature of 50 0 C and relative pressure of 0.5 bar. As already noted, recovery of the excess alcohol takes place continuously. More specifically, the undesired alcohol in the alkyl ester solution may be separated by distillation. A small part thereof remains in the aqueous solution of raw glycerine, from which it can still be 20 recovered later. In view of the above, if the starting material is not already.a refined oil, the integrated process proposed according to the present invention envisages a pre-treatment of depuration and refining of the starting oil, in order to arrive at a dried refined oil regardless of whether the process starts with a raw virgin 25 oil or with used frying oils and/or animal fats. If the starting material is already a pure, already refined, vegetable oil, the only preliminary treatment envis aged before transesterification is drying. The aforesaid preliminary treatments are intended to remove extrane ous substances (proteins, rubbers, resins, phosphates, ketones, aldehydes) 30 which may be present either in suspension or in solution and that can nega tively influence the transesterification process or combustion. More specifi cally, in the preliminary refining of the oil, it is worth removing any lecithin and -10 any free fatty acids, in order to obtain a starting material with consistent char acteristics. According to a preferred embodiment of'the present invention, the said preliminary treatment 1) of depuration of ingredient i), i.e. raw vegetable 5 oil, includes operations of centrifugation, filtration and mucilage removal. The depuration treatment removes most of the water, impurities in suspension and the mucilage, that can generate rubbers. In particular, centrifugation removes the water residues, coarse impurities, fragments of seeds, flours, carbon resi dues, and inhibits the onset of enzymatic reactions. Filtration, obtained with 10 filter-presses, removes all the substances in suspension not removed by cen trifugation. Demucilagination or degumming removes hydratable polar lipids (phospholipids, lipoprotids, glycolipids), resins and rubbers. Still according to a preferred embodiment of the present invention, the preliminary treatment 1) of depuration of the raw vegetable oil includes neu 15 tralisation and winterizing operations. With refining' there is firstly a neutralisa tion or de-acidification of the starting oil, enabling the removal of free fatty acids that are formed in the raw material through lipase activity. This treatment is carried out by adding suitable quantities of bases, particularly sodium hy droxide, to the raw oil. The neutralisation of the free fatty acids partly leads to 20 forming soaps, which may incorporate considerable fractions of neutral oil. As already noted, the integrated process according to the present invention may use biomethanol instead of methanol or bioethanol instead of ethanol, in order to obtain a product with the utmost environmental compatibil ity. Mixing Bio-oil with traditional fuel in suitable percentages according to the 25 type of use and apparatus enables attributing - in the same percentages - the characteristics of environmental compatibility of Bio-oil to the resulting mixture. According to a further aspect thereof, the present invention also pro vides a new biofuel or biocombustible mixture consisting of variable quantities of: 30 I) fatty acid alkyl esters obtainable by transesterification starting from lipid based vegetable or animal materials subjected to preliminary treat ments involving drying, and from lower alcohols or bioalcohols.

11) lower alcohols or bioalcohols or their mixtures. According to a first possibility, the said quantity 11) of lower alcohols or bioalcohols corresponds to the excess alcohols or bioalcohols initially found in the said transesterification operation. In this case, there is no need for opera 5 tions envisaging the separation of the alcohol from the alkyl ester phase pro duced via transesterification. Depending on requirements of use, the quantity 11) of lower alcohols or bioalcohols may also be smaller than the excess alcohol or bioalcohol present initially in the said transesterification operation, and this means that, in produc 10 tion, there will be at least a partial separation of the alcohol contained in the alkyl ester mixture produced, such as by rapid evaporation (flash) of the alco hol, which is the lightest component, from the product mixture. Alternatively, when the mixture according to the present invention must be used, for example, in extreme conditions in aeronautical applications 15 in order to maintain Bio-oil fluidity and to avoid separations, the quantity 11) of lower alcohols or bioalcohols may be greater than the excess alcohol or bioal cohol initially present in the said transesterificatioh operation. In which case, as noted, the final mixture is obtained by adding further alcohol or bioalcohol after the transesterification operation. 20 As will be evident from the data presented below, the process accord ing to the present invention offers a product of higher quality and purity com pared to conventional processes, with lower residual glycerol content and humidity, and yielding a glycerine by-product directly of 95-98% purity. The specific features of the present invention, as well as its advan 25 tages and relative operative modalities, will be all the more evident with refer ence to the detailed description presented merely for exemplificative purposes below, relating to one of its preferred embodiments. The same is illustrated in the attached drawings, wherein: Figure 1 shows an overall block diagram 6f an integrated process for 30 the production of biofuels and biocombustibles according to the present inven tion; Figure 2 shows a block diagram of only that section of the process of -12 Figure 1 concerning the preliminary treatment of used frying oils and animal fats; Figure 3 shows a block diagram of that section of the process of Fig ure 1 concerning the production of the mixture according to the present inven 5 tion starting from pre-treated and dried oil. As shown in the block diagram of Figure 1, the process according to the present invention mainly consists of three sections of preliminary treat ment of the starting material. These three sections are interconnected and can be used either together or alternatively to one another, depending on the type 10 of starting material to be processed and on the characteristics required of the final product. According to the present invention, the oil used for the trans esterification process is obtained from raw, refined or used (frying) vegetable oils and from oils of animal origin. The raw vegetable oils are extracted from oil-producing plant species (colza, sunflower, hemp, sorghum, coconut, soy, 15 palm, etc.) or from algae and/or microalgae produced in aquaculture and/or in thermal bioreactors. The third section of the process, which concerns treatment of the spent food oils, is also shown in more detail in the block diagram of Figure 2. The production lines of all three sections converge in the point indi 20 cated as "Dried refined oil", from which the transesterification process starts, with the subsequent operations of separation and recovery of the various streams and the possible addition of lower alcohol to the Bio-oil obtained in the process. The identity and preferred doses of the various reagents are shown in 25 Figure 1, while the central section of the process that carries out transesterifi cation, the separation of the produced streams and any mixing with additional alcohols or bioalcohols is also shown in more detail in the block diagram of Figure 3. EXAMPLE 30 To obtain a total of 1,000 kg of Bio-oil by means of the process of the present invention, the preliminary treatment is carried out as follows.

-13 Raw vegetable oil If raw virgin vegetable oil is used as a starting material, with a starting quantity of 1,040 kg, the procedure is as follows: a) pre-treatment of depuration; 5 b) pre-treatment of neutralisation with H 3

PO

4 ard NaOH in order to extract soaps and dry matter; c) drying treatment, which yields dried refined oil. The dried refined oil is the nodal point (at the centre of the diagram of Figure 1) of Bio-oil production, which is the arrival point for all the starting 10 materials taken into consideration. Raw vegetable oil and used frying oil Starting from 1,039 kg of starting material, composed of 907 kg of raw vegetable oil mixed with 132 kg of used frying oil (UFO), or oil deriving from animal fats, the procedure is as follows: 15 a) for UFO and oil from animal fats, there is a pre-treatment of centrifuga tion and filtration, drying and esterification with H 2

SO

4 and metha nol/biomethanol or ethanol/bioethanol; b) for raw vegetable oil, there is a pre-treatment of neutralisation with

H

3

PO

4 and NaOH, to extract the soaps and 61ry matter; 20 c) drying treatment yielding the dried refined oil. Refined vegetable oil and used frying oil Starting from 1,009 kg of starting material, composed of 877 kg of refined vegetable oil mixed with 132 kg of used frying oil (UFO), or oil deriving from animal fats, the procedure is as follows: 25 a) for UFO and oil from animal fats, there is a pre-treatment of centrifuga tion and filtration, drying and esterification with H 2

SO

4 and metha nollbiomethanol or ethanol/bioethanol. b) drying treatment yielding the dried refined oil. Refined vegetable oil 30 Starting from 1005 kg of refined vegetable oil as starting material, the procedure is as follows: a) drying treatment yielding the dried refined oil.

- 14 In the production process, starting from the various combinations of the aforesaid starting materials, after the above preliminary treatments the transesterification reaction is carried out. Then treatments of purification and extraction of undesired components, the addition of components necessary for 5 particular uses (methanol and/or biomethanol, ethanol and/or bioethanol) are carried out, to finally arrive at Bio-oil, as shown in the diagram of the process. To produce 1,000 kg of Bio-oil, considering the entire process, the following chemicals and relative quantities are used: 10 CHEMICALS MIN (kg) MAX (kg) Biomethanol 0 * 450 Methanol 0* 450 Bioethanol 0* 450 Ethanol 0* 450 Sodium methylate 5.0 10.5 Citric acid 0.5 1.5 96% sulphuric acid 0.5 . 1.7 36% hydrogen chloride 13.0 15.5 80% phosphoric acid 1.5 3.00 50% caustic soda 10.5 13.7 * The four products are combined according to the optimal percentages nec essary for the type of starting material and for the type of Bio-oil to be pro duced. For minimum environmental impact, the process will use biomethanol and bioethanol in suitable proportions. 15 Table 1 below reports some characteristics of biodiesel for motor vehicles according to UNI EN 14 424 specifications, in comparison with the Bio-oil produced according to the procedure of the present invention. 20 (Table follows) 15 00 o ZZ CLV) 0 -. zzz 0 0 CD 09 ? A U) , 01 w Fn sO 00 00 0D 0 CO 0) 0 TA c 00 CL ~ ) 0 0 0 N0C )0 C 0 0 0 0 ( z LO 0 ~ 00 0) < C) C-N6 ' ow 0- z m 0 co -E o 0 0 o E E -)d.1 E E ~EEE E MD 0 000 0~ 0 00 0 0 0 E 0 0) '.0) C 0) (D w. 0 E o 0 0 0 -C o (D 0 0 0 OO L' L L) 6)1 2.1 n r w -L La c~ z 16 V 0 OD) 0)

I'

I- LWWWLJWWUWWWWWW "W -J 0 CD 0 00004 (n o w -7"9c"P" CO 8 EE -I -0. - - - C. C +4 o 00 ) z ' 0 w 0 C D0 0 A c0 ()6-( c :E -a, ch 0) cm~~ *0.: 0 cm.m a -o 0 0 w i~DI- 8 U- 0-LL CL 0~ -.17 From the above data, as well as from what is already known in the field of combustibles/fuels obtained from biomasses, it appears that the mix tures according to the present invention (Bio-oil) represent a biofuel of very low environmental impact. Even when mixed with fossil diesel fuel, it does not 5 lose its biocompatibility, but the mixture itself enhances its own positive char acteristics as a function of the percentage of Bio-oil used. The direct and indirect advantages of the biofuel include safety of use, due to its high flash-point of over 1 10*C, and its high biodegradability in soil or water, which is maintained in the corresponding percentage even when mixed 10 with fossil diesel fuel. Moreover, the biofuel mixture according to the present invention al lows reducing nearly all levels of emission, also with respect to biodiesel, which already presents considerable advantages in this regard. In particular, carbon monoxide and non-combusted residues are lower because using alco 15 hol lowers the combustion temperature, and the presence of oxygen in the alkyl ester molecule contributes to a better combustion. The carbon dioxide produced by Bio-oil, owing to its vegetable origin, is compensated by the carbon dioxide absorbed by the plants grown for the production of the starting oil. As regards this advantageous effect, there is, for 20 example, an average reduction of 2.5 tonnes of CO 2 emitted for each tonne of fossil diesel replaced. As with other biofuels, the vegetable origin of Bio-oil guarantees the absence of heavy metals and, since it does not contain sulphur, it reduces pollutants, does not contribute to acid rain and increases the efficiency and 25 duration of catalysts of transport vehicles and of industrial plants. There are also no aromatic polycyclic hydrocarbons, which are highly cancerogenous. Moreover, there is a considerable decrease in mutagenicity values of PM10 fine particulate emissions, especially in the most harmful part, the car bonious one. The carbonious part is the one that is absorbed the most during 30 respiration and is difficult to block in catalysts in industrial plants and transport vehicles. In a different and more advantageous manner with respect to bio- -18 diesel, Bio-oil associates the known detergent and lubricant properties of alkyl ester combustibles (biodiesel) and the slightly corrosive properties of alcohols, thereby enhancing the safety, reliability and efficiency of systems. The deter gent property of Bio-oil, which means a considerable reduction'of industrial 5 plant dirtying, leads to less frequent maintenance work for some components as well as greater safety and reliability owing to better system functioning. In particular, those critical components of the apparatus that are par ticularly critical for efficiency are kept clean: namely, the areas where chemical reactions take place and where there is oxidation linked to energy production, 10 as in the case of fuel cells, turbines, internal combustion engines and burners. The same beneficial detergent, lubricant and slightly corrosive effect is ob tained for apparatus components where the biofuel passes through or remains in, such as nozzles, conduits, injectors, piping, tanks etc. In short, Bio-oil has the following advantageous characteristics: 15 - a high flash-point of over 1100 C - high biodegradability in soil or water, of over 99.5% after 20 years - an average reduction of CO 2 emission on overall balance - a reduction of fine particulate (PM10) of 58%; a reduction of 76% of the carbonious part of fine particulate (soot) and a resulting reduction of the 20 mutagenicity values for the particulate. - greater oxygen content, of about 11 % with respect to fossil diesel fuel. - no aromatic polycyclic hydrocarbons, heavy metals or sulphur. - a 58.% abatement of carbon monoxide emissions at high loads. - a decrease in aromatic compounds of up to 68%. 25 - a detergent and lubricant action on system components. The present invention has been disclosed with reference to some specific embodiments thereof, but it is to be understood that variations or modifications can be brought by persons skilled in the art without departing from the scope of the appended claims. 30

Claims (13)

1. A process for the production of biocombustible and biofuel mixtures suitable for different conditions of use, comprising the following fundamental 5 operations: a) producing mixtures of fatty acid alkyl esters and glycerine by trans esterification, starting from lipid-based vegetable or animal materials and from lower alcohols or bioalcohols in excess; b) separating the mixtures deriving from the said operation a) of trans 10 esterification into a phase based on raw glycerine and a phase contain ing the said mixtures of fatty acid alkyl esters and the excess amount of lower alcohols or bioalcohols; characterised by the fact that the said starting lipid-based vegetable or animal materials include one or more of the following ingredients: 15 i. raw vegetable oil ii. refined vegetable oil iii. used food oil and/or animal fats and by the fact that the said ingredients undergo the following preliminary treatments upstream of said operation a) of transesterification: 20 1) the said ingredient i), raw vegetable oil, is subjected to a prelimi nary depuration and refining treatment in order to remove impuri ties and to neutralise and winterize it, and then to drying of the re fined oil thus obtained; 2) the said ingredient ii), refined vegetable' oil, is subjected to prelimi 25 nary drying; 3) the said ingredient iii), used food oil and/or animal fats, is sub jected to a preliminary depuration treatment, to drying and then to an esterification of the free fatty acids contained therein, by addiion of lower alcohols or bioalcohols; the obtained product based on 30 fatty acid alkyl esters is mixed in a proportion of not more than 20% with dried refined oil obtained from treatments 1).or 2) above.

2. A process according to claim 1, wherein, after the said operation b) - 20 of separation, the phase containing said mixtures of fatty acid alkyl esters and the excess amount oflower alcohols or bioalcohols is subjected to a further separation treatment for the separation of amounts ranging from 0 to 100% of the said alcohols or bioalcohols present after the said operation b) of separa 5 tion.

3. A process according to claim 1, wherein, after the said -operation b) of separation, the phase containing said mixtures of fatty acid alkyl esters and said excess amount of lower alcohols or bioalcohols is not subjected to further separation treatments, and the whole excess quantity of lower alcohols or 10 bioalcohols is kept in the final product.

4. A process according to claim 1, wherein, after the said operation b) of separation, an additional amount of lower alcohols or bioalcohols is added to the phase containing the said mixtures of fatty acid alkyl esters and the said excess lower alcohols or bioalcohols. 15

5. A process according to any one of claims 1-4, wherein the said lower alcohols or bioalcohols are selected from the group consisting of metha nol, ethanol, biomethanol, bioethanol and their mixtures.

6. A process according to any one of claims 1-5, wherein the said operation a) of transesterification is carried out with an alkaline catalyst. 20

7. A process according to claim 6, wherein the said operation a) of transesterification is carried out in three consecutive stages in which the said alcohols or bioalcohols and the said catalyst are dosed and recycled at every stage.

8. A process according to claim 1, wherein the said preliminary treat 25 ment 1) of depuration of ingredient i), raw vegetable oil, includes operations of centrifugation, filtration and demucilagination.

9. A process according to claim 1, wherein the said preliminary treat ment 1) of depuration of ingredient i), raw vegetable oil, includes neutralisation and winterizing operations. 30

10. A biocombustible or biofuel mixture consisting of variable amounts of: 1. fatty acid alkyl esters obtainable by transesterification starting from -21 lipid-based vegetable or animal materials subjected to preliminary treatments including drying, and from lower alcohols or bioalcohols.

11. lower alcohols or bioalcohols or their mixtures. 11. A mixture according to claim 10, wherein the said amount II) of 5 lower alcohols or bioalcohols corresponds to an excess alcohol or bioalcohol initially present in the said transesterification process.

12. A mixture according to claim 10, wherein the said amount 1I) of lower alcohols or bioalcohols is greater than an excess alcohol or bioalcohol initially present in the said transesterification process, and is obtainable in the 10 said mixture by addition after the said transesterification process.

13. A mixture according to claim 10, wherein the said amount 1I) of lower alcohols or bioalcohols is smaller than an excess alcohol or bioalcohol initially present in the said transesterification process.