Abstract:
The “MOBILE PLANT FOR SELF-SUSTAINABLE BIODIESEL PRODUCTION AND MOBILE PROCESS FOR BIODIESEL PRODUCTION” characterized by a compact equipment arrangement for the biodiesel production in a way intended to reduce waste generation and, additionally, allow reuse/application of some of them; it is organized and arranged over a chassis with axle and wheels that can be attached and taken to various locations, presents a self-sustainable format to use its own fuel to generate electricity to supply the entire plant, if necessary.

Description:
[0001]    This procedure aims to provide a feasible technical way to produce biodiesel fuel from renewable sources, to meet the proposed demands of the National Program for Biodiesel Production and Use, PNPB, launched and promoted by the Brazilian Federal Government. This is a route and metric of production that provides the security demanded for the equipment operation involved, and use of products obtained. 
         [0002]    The Mobile Biodiesel Plant, designed and developed with focus on sustainable energy, has its technical pillars secured by its own scientific research and foundations in international scientific literature. 
         [0003]    Having energy and environmental sustainability as its primary object, the process seeks to establish a route and equipment for biodiesel production from vegetable oils in natura and/or residual, from diverse oilseeds. In order to produce biofuel of interest, it is required as an input, besides the oil chemically known as triglycerides, an alcoholic source, preferably primary short-chained and the use of an acid or basic homogeneous catalyst. 
         [0004]    The mobile character of the production process is the main innovative parameter in accordance with the worldwide state of the technique, allied to innovation over sustainability and self-sufficiency of the unit, once it can be operated in remote areas, even without electricity supply or inputs for a certain period of time. It is noticeable, still, in terms of innovation and sustainability, the matter of application of products from the production process into some processing stages, with the goal of reducing the need for external inputs, besides producing a smaller amount of waste and reducing energy consumption. 
       STATE OF TECHNIQUE 
       [0005]    There are several studies conducted on biodiesel production and processes of different routes have been described, typically making use of batch processes and, eventually, semi-continuous processes with the introduction of expensive technologies that are too complicated to operate, as the microwave or ultrasonic energy. 
         [0006]    An example of this is the patent request U.S. 2002/0074760 A1 which describes a reaction route in which the catalyst is mixed with oil and applied to microwave energy, to force the mixture when there is an adding from the alcoholic source. It has been said that the process is not only capable of producing biodiesel, but also products from fractional distillation, as from gasoline, kerosene. 
         [0007]    The Brazilian application PI 0404243-3 A protects a process of biodiesel production from semi-refined vegetable oil, anhydrous alcohol and alkaline catalyst in heated reaction environment that occurs in two stages. Both occur at temperatures between 60-80° C. when, after the first stage the products are sent to a heating stage to recover the unreacted alcohol by evaporation, followed by its condensation. As soon as the liquid mixture is cooled and separated into two phases, the lighter phase is a mixture of esters and oil and the denser phase is rich in glycerol. Then, the lighter phase is directed to the second reactor, where more alcohol is added according to the need for continuity of the reaction to reach an intended transformation. After that, the catalyst is neutralized with an acid additive. Alcohol in excess is eventually recovered and the phases, products from reaction, separated by decantation or centrifuge. The phase of interest, the lighter one, is washed with a mixture of water and then, strongly heated to remove water incorporated into the organic phase. 
         [0008]    It is important to mention that the process described above has technical flaws regarding the thermodynamics of the reaction in question due to stages named after-treatment of reaction mixture, besides, some procedures used, could affect its economic viability and, later on, have an excessive dependency on external inputs of productive route. 
         [0009]    The Brazilian work patented under the code PI0503631-3A describes a process for biodiesel production especially from castor oil, but applicable to other sources of oil in which the acidic or basic catalytic process, occurs in two stages, the first one being in two vessels in parallel and, after separating the lighter phase from the denser one, the former is directed to a second reactor where they mixture the first tow roll of tanks, for a second reaction stage. The above process highlights the reuse of the catalytic converter available in glycerin, the denser part mentioned, to reduce the emission of wastes. Another point to be highlighted is a concern about the recovery of alcohol, which must be added in excess to the reaction that occurs more quickly and efficiently. This recovery stage is performed after the separation of phases and fuel washing, produced as a purification step. 
         [0010]    This work comes with the idea, maybe even tasteless, to reuse one of its process lines in a following stage, to take advantage of the excessive catalyst in a second of reaction, however the mentioned action may interfere considerably in kinetics reaction, once having the incorporation of a reaction product as an input vehicle. On the other hand, it starts with the idea of not mixing the dense phase, the reaction product, with the washing water, not to jeopardize its following reapplication. This organization proved to be interesting and safe in future procedural routes tested by this group and one of the reasons to develop the distinct work. 
         [0011]    Another recent work, PI0700781-7A is about the production of biodiesel from animal fat, particularly swine, making use of methanol as a source of alcohol. However, it proves to be an inefficient process for the final quality assured to the product as well as what it refers to process timing as a whole. Unlikely, the interest process of the current work is not applied to the conversion of animal fat into biodiesel. The intended focus here may only be applied if that fat is mixed, under heating, with vegetable oil. 
         [0012]    Very well described by the current work, registered under the code PI 0604251-1A, the vegetable oils, when extracted, either by the use of organic solvents or by pressing, carry on their composition not only triglycerides but also some organic acid content due to the presence of free fatty acids. Other possible components of these oils are substances commonly referred to as “non-saponifiable matter”. Intuitively one may realize that these compounds are not converted into biodiesel when there is transesterification, it soon makes necessary the removal of this fraction in order to raise the purity of the final product: biodiesel. One of the applicable processes is named Degumming, for instance. However, some of these compounds should be kept in oil, even when not transformed, but they present some interesting characteristics to oil and to fuel such as oxidation stability, as it is the case of tocopherols and sterols. Unfortunately, removing one of the non-saponifiable compounds, all the others are removed as a consequence. This current work doesn&#39;t deal with the application of the solid part, inherent product from oilseed extraction, but explores a potential application straight in one stage of purification of biodiesel, the main product of interest. 
       SUMMARY OF THE INVENTION 
       [0013]    With all the above techniques and foundation already in place, the objective of the current application is the development of a biodiesel productive route, with emphasis in a process of high technical and economic sustainability environment, added to the feature of mobility of the whole productive process. Additionally, it assumes a prominent position in the market scenario for providing a biodiesel production plant, suitable for small demands of ethanol. Linked to the mobility of the industrial process it can make available for the most remote communities, an innovative process for conversion of raw or fried vegetable oil in a power source for agricultural equipment. 
         [0014]    The process is capable of transforming different vegetable oils just like soybean, sunflower, canola, jatropha, canola and crambe in addition to waste oils, providing the recycling. As alcoholic input it makes use of primary alcohols of low molecular weight in basic or acidic homogenous catalysis process. 
         [0015]    Considering that: 
         [0016]    1. PNBP, National Program of Biodiesel Production and Use, already highlights the necessity of process production in local consumption of biodiesel; 
         [0017]    2. There are numerals oilseeds that provide oil to be transformed into biodiesel; 
         [0018]    3. The oil sources provide considerable quantity of solid wastes, in the process of oil extraction. Those same wastes, for some oilseeds still don&#39;t have safe commercial application; 
         [0019]    4. The purification processes for biodiesel production demand the addition of several new inputs; 
         [0020]    5. The biodiesel production route is a potential generator of co-products. Mostly with low market application up to the present moment; 
         [0021]    6. There is a favorable energy balance for reapplication of certain co-products before an eventual disposal. 
         [0022]    The proposal to have a mobile unit of self-sustainable biodiesel production is to provide an innovative process, adding reengineering concepts and energy coming from waste, described as the following. 
     
    
     DESCRIPTION OF THE INVENTION 
       [0023]    As an initial motivation, the mobile feature is the first and most noticeable inventive factor in question. All the productive process, since the seeds processing, pre-treatment of oil, either raw vegetable or residual, used as the route for biodiesel production, having aggregated a part of storage and tankage, was contemplated. In addition, electric power generating equipment, water tanks and process water, as well as needed infrastructure for instrumentation and equipment control, also preliminary analysis of the product in focus, the biodiesel, were aggregated to the structure. At the processing and oil reaction parts, the tanks and reactors were arranged to take the most of the vertical gap, reducing the necessity for a large number of pumps for circulation of fluid phases. 
         [0024]    As shown in pictures  1  and  2 , respectively, there are the perspective view and the exploded view of the MOBILE PLANT FOR SELF-SUSTAINABLE BIODIESEL PRODUCTION. The plant was designed and built over a movable structure, such as an articulated truck body. In this picture, the truck is being represented only in illustrative form. Over such structure, the equipment and utilities were constructed and organized. To name them: 
         [0025]    1. 02 oil and alcohol storage containers (T 01  and T 02 ), to keep these substances during transport; 
         [0026]    2. Power generator (E 01 ), diesel engine which allows the application of the product that was generated at the plant as an energy source for that same engine. 
         [0027]    3. Unit (E 02 ) continuous extraction of vegetable oilseeds by mechanical pressing. 
         [0028]    4. Oil filtration unit (E 03 ), with a semi continuous operation, to remove suspended solids and container for eventual pH correction or addition of drying agent or flocculants, if necessary; 
         [0029]    5. On the left, (E 04  and E 05 ) electric control equipment panels; 
         [0030]    6. Besides 04 tanks made of stainless steel, for storage and oil supply in natura (T 03 ), residual (T 04 ) alcohol tanking (T 05 ) and at last biodiesel storage (T 06 ) already produced and polished; 
         [0031]    7. At the middle right, the reactors and processing utilities from front to rear, all made of stainless steel. To name them:
       7.1 First reactor (T 07 ) with heating (A 01 ) and temperature control between ambient temperature and 80° C., besides agitation controlled by frequency converter limited between 450 and 1000 rpm;   7.2 First Settling tank (T 09 )   7.3 Second reactor (T 08 ), the same as item 7.1, with heating (A 02 ) and agitation controlled;   7.4 Second Settling tank (T 10 )   7.5 Storage (T 12 ) of the dense phase, glycerin, with heating (A 03 ) limited to 100° C. with outlets for liquids at the base and for gases at the top,   7.6 Third Settling tank (T 11 )   7.7 Purification tank (T 13 ) of the esters mixture and as the storage tank at 7.5, with controlled heating (A 04 ) and with outlets for liquids at the base, and for gases at the top;   7.8 Heat exchanger (E 06 ) of tubes operated in counter-current;   7.9 Clean water passage box (T 14 )   7.10 (T 15 ) Heating storage of clean water for the process, with a limit of 80° C. in temperature rising;   7.11 liquid-liquid extraction column (T 16 ) for removing water soluble impurities from biodiesel;   7.12 Drying column (T 17 ), with heating (A 06 ) controlled between ambient temperature and 100° C., besides vacuum system (B 08 ) controlled from ambient pressure to 100 mmHg, for final biodiesel polishing;       
 
         [0044]    8. Office (ES) for organization and laboratory work; 
         [0045]    9. Cabinets and laboratories of physic-chemical analysis of the primary product. 
         [0046]    The entire set is equipped with lighting system, emergency exits and fire extinguishers suitable for the structure in question. The process of biodiesel production represents in picture  03 : 
         [0047]    Flowchart of the mobile process for biodiesel production designed and built over a mobile handset. 
         [0048]    In the beginning of the production process from the oilseed, that same seed is mechanically pressed (E 02 ) for vegetable oil extraction, resulting in a vegetable oil with high solid contents, and a pie, solid part with low oil remaining. In the next stage, the oil is filtered (E 03 ) and if necessary has its pH corrected before reaching the mobile-power-pump (B 07 ). From this stage the oil can go to the tank (T 01 ) of vegetable oil in natura storage. Eventually when processing residual oil, it has the beginning of its process with the filtration (E 03 ) and in sequence it is directed to tanking (T 02 ). Later, the oil is powered by pumping (B 01 ) in one of the reactors (T 07  or T 08 ), that work in parallel, and may, if needed, undergo a process of pre-treatment or refining, in the first reactor (T 07 ) for the removal of chemical components that are not wanted in the final product. Then it goes to a decantation stage (T 09 ) of the phases, the lighter one being the one of interest. The oil, eventually well treated, follows to the second reactor (T 08 ) in which alcohol will be added by pumping (B 020 ), under heating (A 02 ) and strong agitation to force the mixing of the two phases. As soon as the catalyst is added and, under the control of temperature, its reaction is developed. 
         [0049]    Once the inputs react, biodiesel and glycerin are produced, and must be split. Due to considerable density differences, the process can be performed by decantation (T 09 , T 10  or T 11 ), with gravity aid, searching for energy and space economy. 
         [0050]    The phases are split in different tanks. The light fraction, fatty esters, is directed to the purification tank (T 13 ), and the heavy fraction, rich in glycerin and alcohol is directed to the storage (T 12 ) of the dense phase. An independent heating system (A 03  and A 04 ) is activated for alcohol evaporation that is prominent from the excess of the reaction phase, to increase the efficiency and reaction kinetics. Under heating, the alcohol is evaporated in: dense phase storage (T 12 ) and purification tank (T 13 ) and subsequently condensed in the heat exchanger (E 06 ) of parallel tools in countercurrent to liquid cooling. Alcohol returns to its original tank ready for further application in the next process without waste generation at that stage. 
         [0051]    For co-solubility, a small fraction of glycerin was transported during the lighter phase due to the alcohol that was solubilized and that once was just removed by evaporation. The removal of that small impurity fraction in a process of liquid-liquid extraction (T 16 ) soon becomes simple, having oil as its stationary phase; heated water is added to the column, that suffuses the organic lighter phase. 
         [0052]    For not mixing, the organic ester phase and the water split by Settling tank (T 16 ), the water set aside for the biodiesel (still under purification). Once they are split, the water is stocked (T 18  and T 19 ) for post application. The biodiesel with a small incorporated humidity is directed to a drying column (T 17 ) where, with heating and pressure reduction by an operation vacuum pump (B 08 ), the water is withdrawn and released as vapor into the environment. The biodiesel, dry, is ready for tanking (T 06 ) and use as fuel, applied pure or in fractions of a mixture with mineral diesel. 
         [0053]    An innovation proposed on the described route refers to the application of glycerin (retained in T 12 ) as an additive on the coolant heat exchanger (E 06 ). The glycerin, that initially has no direct application on the process, starts working as a heat transfer material, to condense evaporated alcohol in (T 12 ) and (T 13 ) returning the same to alcohol storage tank (T 05 ). As the glycerin is completely soluble in water it can be solubilized in this one and exchange heat from alcohol vapor. 
         [0054]    This organization and arrangement provides a relative compact industrial structure achieving a high level of operation performance and efficiency. It is added to the security, already mentioned, and durability of the plant, due to damping systems and connections developed, reducing the strictness of the system, warning about the appearance of cracks and wear out of equipment due to the unit transport. Once assembled, the equipments are perfectly integrated with components connected by flexible joints and flanges. Therefore, the mobile plant, despite having a small size for a plant, puts itself into an inventive character of an innovative model of production able of reaching diverse locations with safety, durability and quality in the processing system. 
       Example 1 
       [0055]    Cold pressed oilseeds are received (E 02 ) for mechanical extraction of vegetable oil in natura and thrown into the filter press (E 03 ) from which tanking pumps follow (T 03 ). 100 kg of oil for reactor (T 07 ) is directed for pumping (B 01 ) where it is heated under 55° C. and mixed in 31 kg alcohol, directed by pump (B 02 ), from its tank (T 05 ), and 4.5 kg of catalyst added manually. Under strong agitation, the mixture remains for 45 minutes. It is directed by pump (B 03 ) to separation phases (T 11 ) where it is kept it remains in rest for one hour and from there directs the inferior phase by gravity to glycerin tanking (T 12 ) and the lighter phase to purification (T 13 ) where the excess of alcohol will be evaporated by heating (A 03  and A 04 ) under 75° C. for 40 minutes. The retained material in tank is directed, by pump (B 04 ), to washing (T 16 ) where it is pulverized by pumping (B 05 ), heated water (T 15 ) at 50° C. and remains for phase separation for 30 minutes. The tanking water and the lighter phase for drying (T 17 ) at 100° C. and at 0.80 atm of pressure for 25 minutes. The biofuel, ready for tanking is directed by pumping (B 06 ). 
       Example 2 
       [0056]    Frying oil is received and thrown into the filter press (E 03 ) from which follows by pumping (B 01 ) for tanking (T 04 ). 100 kg of oil for the reactor is directed by pump, (T 07 ) where it is heated (A 01 ) at 60° C. and mixed with 35 kg alcohol, directed by pump (B 02 ) from its tank (T 05 ), and 5 kg of catalyst added manually. Under strong agitation, the mixture continues for 15 minutes. 100 kg of oil are directed to reactor (T 07 ) where it is heated (A 01 ) ate 60° C. and mixed with 35 kg of alcohol directed by pump (B 02 ) from its tank (T 05 ) and 5 kg of catalyst, directs by pump (B 03 ) for phases separation (T 09 ) where it is kept in rest for an hour and from there directed by gravity the inferior phase for 30 minutes. It is directed by gravity the water for tanking (T 18 ) and the lighter phase for drying (T 17 ) at 100° C. and at 0.90 atm of pressure for 30 minutes. It is directed by pumping (B 06 ) the biofuel ready for tanking (T 06 ).