MXPA05010046A - Fuel production - Google Patents

Abstract

An apparatus that includes a first reactor and a return mechanism. The fir st reactor has an inlet to receive a mixture comprising a first reactant, a second reactant, a reaction product, and an inert solvent that dissolves at least a portion of the first and second reactants, an enzyme to facilitate a reaction between the first and second reactants to generate more reaction product, and an outlet to output the reaction product, including the reaction product received at the inlet and the reaction product generate d from the reaction between the first and second reactants. The return mechanism sends at least a portion of the reaction product from the outlet back to the inlet.

Description

FUEL PRODUCTION REFERRAL TO RELATED REQUESTS This application is a continuation in part of the US Application. No. 10 / 945,339, filed on September 20, 2004, entitled "Methods to Produce Alchol Esters," for Chih-Chung Chou, the contents of which are incorporated here by reference.

BACKGROUND This invention relates to the production of fuel, including the production of bio-diesel fuel from vegetable oils and animal fats. A source of alcohol oils from vegetable oils and animal fats can be used to produce alkyl fatty acid esters, which can be used as diesel fuels, generally referred to herein as "bio-diesel" fuels. In an approximation of production, non-enzymatic catalysts, such as alkali hydroxides and alcoholates, are used to facilitate alcoholysis. A by-product of alcoholysis is glycerol. The non-enzymatic catalysts are removed with the glycerol and can not be re-used. The purification of glycerol becomes difficult because it contains a large amount of the catalyst. In another production approach, enzyme catalysts, such as lipases, are used to facilitate the production of alkyl esters of natural oils in an alcoholysis reaction. A source of oil containing triglyceride and an alcohol are dissolved in an organic solvent. With a lipase as a catalyst, the triglyceride and the alcohol react to produce alkyl ester, with glycerol as a by-product.

BRIEF DESCRIPTION OF THE INVENTION In a general aspect, an enzymatic trans-esterification approach for the production of bio-diesel fuel provides a high purity fuel, such as an alkyl ether (and in some examples, glycerol sub-product), a cost efficient way, with less expense and reduced side product. The processing plant for enzymatic trans-esterification can be done using a simple configuration that requires reduced capital investment. In general, in one aspect, the invention shows an appus that includes a first reactor having an inlet for receiving a mixture comprising a first reagent, a second reagent, a reaction product and an inert solvent that dissolves at least a portion of the first and second reagents, an enzyme to facilitate a reaction between the first and second reagent to generate more reaction product, and an exit to remove the reaction product, including the reaction product received at the inlet and the reaction product generated from the reaction product. the reaction between the first and second reagent. The appus includes a return mechanism for sending at least a portion of the reaction product from the outlet and back to the entrance. The implementations of the invention could include one or more of the following features. The reaction product includes alkyl ester. The return mechanism sends at least a portion of the alkyl ester back to the inlet. The mixture includes a solvent that dissolves at least one portion of the first reagent, the second reagent and the reaction product. The outlet produces at least the alkyl ester, the solvent and the first unreacted reagent. The appus also includes an evaporator to evaporate the solvent to generate a mixture that includes the alkyl ester and the first unreacted reagent. The output also produces glycerol. The appus also includes an evaporator to evaporate the solvent to generate a mixture including the alkyl ester, the glycerol and the first unreacted reagent. The appus also includes a phase sepor for seping the alkyl ester from the glycerol based on the liquid-liquid phase sepion. The first reagent includes triglyceride. The first reagent includes a carboxylic acid. The second reagent includes at least one of a primary and secondary alcohol. The first reagent includes at least one of, vegetable oil and animal fat. The reaction product has a composition that is suitable for use as fuel. The reaction product has a composition that is suitable for use as fuel for a diesel engine. The reaction product has a composition that is suitable for use as fuel for at least one internal combustion diesel engine and a gas turbine diesel engine. The apparatus also includes a mixer having a first inlet for receiving the first reagent, a second inlet for receiving the second reagent, a third inlet for receiving a portion of the reaction product from the reactor outlet, a fourth inlet for receiving the solvent inert and an outlet to produce the mixture including the first reagent, the second reagent, the inert solvent and the reaction product. The output also produces other components and the return mechanism also sends at least a portion of the other components back to the input. The enzyme facilitates a reaction between the other components and the second reagent to generate more reaction product. The other components include at least one monoglyceride, di-glyceride, triglyceride and carboxylic acid. The apparatus also includes a second reactor having an inlet to receive a mixture including second additional reagent and reaction product from the outlet of the first reactor from the outlet of the first reactor, an enzyme to facilitate a reaction between the second reagent and the others components to generate more reaction product and an output to produce the reaction product, including the reaction product received at the inlet of the second reactor and the reaction product generated from the reaction between the second reagent and the other components.

The apparatus also includes an evaporator for evaporating the inert solvent and at least one of the first unreacted reactants and second unreacted reactants. The apparatus also includes a short path evaporator for separating the reaction product from the remaining unreacted reagent. The reaction product includes alkyl ester. The reaction product includes at least 99% alkyl ester. The apparatus also includes a return mechanism for sending at least a portion of the alkyl ester from the outlet of the second reactor back to the entrance of the first reactor. The first reagent includes triglyceride or carboxylic acid and the second reagent includes primary or secondary alcohol. In general, in another aspect, the invention shows an apparatus that includes a reactor having an inlet for receiving a mixture including reagents, an enzyme for facilitating a reaction between the reagents and a regeneration mechanism for sending at least a portion of a product of the reaction back to the entrance. The implementations of the invention could include one or more of the following features. The product of the reaction includes alkyl ester and the regeneration mechanism sends at least a portion of the alkyl ester back to the inlet. The reagents include (1) at least one of the triglycerides and carboxylic acid and (2) at least one of the primary and secondary alcohols. The enzyme includes a lipase. In general, in another aspect, the invention shows a system for generating alkyl ester that includes a first subsystem and a second subsystem. The first subsystem includes a first reactor having a first inlet to receive a first mixture that includes a first reagent, a second reagent and an inert solvent to dissolve the first and second reagent, a first enzyme to facilitate a reaction between the first and second reagent to generate a reaction product and a first outlet to produce the reaction product, the inert solvent and other components. The second subsystem includes a second reactor having a second inlet to receive a second mixture including second additional reagent, an inert solvent, at least a portion of the reaction product and the other components of the exit, a second enzyme to facilitate an reaction between the second reagent and the other components to generate more reaction product and a second exit to produce the reaction product, including the reaction product received at the entrance of the second inlet and the reaction product generated from the reaction between the second reagent and the other components. The implementations of the invention could include one or more of the following features. The reaction product includes alkyl ester. The system also includes a return mechanism for sending at least a portion of the alkyl ester from the first outlet back to the first entrance. The system also includes a return mechanism for sending at least a portion of the alkyl ester from the second outlet back to the entrance. The percentage of alkyl ester in the reaction product at the outlet of the second reactor is greater than the percentage of alkyl ester in the reaction product at the outlet of the first reactor. The second subsystem includes a separator for removing at least a portion of non-alkyl ester components from a first solution outlet of the second outlet to obtain a second solution having at least 90% by weight alkyl ester. The separator includes an evaporator. The separator includes a liquid-liquid separator. The first subsystem includes a separator for removing at least a portion of components, which are not alkyl esters, from a first solution outlet of the first outlet to obtain a second solution having a higher concentration of alkyl ester than the first solution. The separator includes an evaporator. The separator includes a liquid-liquid separator. In some examples, the first reagent includes triglyceride. In other examples, the first reagent includes carboxylic acid. The second reagent includes at least one of the primary and secondary alcohols. The first subsystem includes a mixer having a first inlet for receiving the first reagent, a second inlet for receiving the second reagent, a third inlet for receiving the inert solvent, a structure for mixing the first reagent, the second reagent and the inert solvent and an output to produce the first mixture including the first reactant, the second reactant and the inert solvent. In some examples, the first enzyme is equal to the second enzyme. In other examples, the first enzyme is different from the second enzyme. At least one of the first and second enzymes includes a lipase. In general, in another aspect, the invention shows an apparatus that a reactor, a separation unit and a return mechanism. The reactor has a line of tubing for transmitting a mixture that includes a first reagent, a second reagent, an inert solvent and a reaction product that are in homogeneous state, a coupler for receiving a cartridge having an inlet to receive a mixture from the line of tubing, an enzyme to facilitate a reaction between the first and second reagent to generate more reaction product and an exit to produce the reaction product, including the reaction product received at the inlet and the reaction product generated from the reaction between the first and second reagent. The separation unit processes the production of the output to produce a solution that has a higher percentage of the reaction product. The return mechanism sends at least a portion of the solution back to the pipeline. In general, in another aspect, the invention shows a system for generating alkyl ester includes a first subsystem and a second subsystem. The first subsystem includes a first reactor having a first line of tubing for transmitting a first mixture that includes a first reagent, a second reagent, an inert solvent and alkyl ester that are in a homogeneous state, a first coupler for receiving a first cartridge having a first inlet to receive the mixture from the first line of pipe, a first enzyme to facilitate a reaction between the first and second reagent to generate alkyl ester and a first outlet to produce the alkyl ester, the solvent and other components. The second subsystem includes a second reactor having a second pipeline for transmitting a second mixture including second additional reagent, inert solvent and at least a portion of the alkyl ester and the other components from the first outlet, a second coupler for receiving a second reactor. second cartridge having a second inlet to receive the mixture from the second line of pipe, a second enzyme to facilitate a reaction between the second reagent and the other components to generate more alkyl ester, and a second outlet to produce the alkyl ester. In general, in another aspect, the invention shows a system for generating alkyl ester that includes a cartridge for receiving a mixture that includes a first reagent and a second reagent, the cartridge including an enzyme to facilitate a reaction between the first and second reagent for generate a reaction product, the cartridge has an identifier; and a regulator for controlling a condition of system operation based on the identifier in the cartridge. The implementations of the invention could include one or more of the following features. The reaction product includes alkyl ester. The enzyme includes a lipase. The regulator controls a speed of a pump based on the identifier, in which the speed of the pump affects the speed at which the solution passes through the cartridge. The regulator controls a heater based on the identifier, in which the heater affects a temperature of the solution. The regulator determines when to send a signal indicating that the cartridge needs to be replaced based on the identifier. In general, in another aspect, the invention shows an apparatus that includes a first reactor having an inlet to receive an oil source and a reagent and an enzyme to facilitate a reaction between the oil source and the reagent to generate a desired product. and other components; and a first separator for separating the desired product from the other components to generate a desired crude product; and a return mechanism for sending at least a portion of the desired crude product back to the entrance of the first reactor. The implementations of the invention could include one or more of the following features. The desired product includes a fuel. The desired product includes alkyl ester. The apparatus also includes a second reactor having an inlet for receiving a mixture including additional reagent and at least a portion of the desired crude product and an enzyme to facilitate a reaction between the reagent and components in the desired crude product to generate additional desired product.; and a second separator for separating the desired product from other components to generate a desired high purity product. The source of oil includes at least one of the triglycerides and carboxylic acid. The crude fuel includes alkyl ester. The reagent includes at least one of the primary and secondary alcohols. The enzyme includes lipase. In general, in another aspect, the invention shows an apparatus that includes a cartridge including an enzyme, the cartridge is configured to be coupled to an alkyl ester generator. The alkyl ester generator includes a mixer that mixes a first reagent, a second reagent, an inert solvent and alkyl ester to generate a solution that is passed through the cartridge, in which the enzyme in the cartridge facilitates a reaction between the first and second reagent for generating more alkyl ester, and a return mechanism for sending at least a portion of the alkyl ester derived from the reaction between the first and second reagent back to the mixer. The implementations of the invention could include one or more of the following features. The enzyme includes a lipase. The cartridge includes information in the cartridge related to an operation of the alkyl ester generator. In general, in another aspect, the invention of our apparatus includes a cartridge including an enzyme, the cartridge is configured to be coupled to a first subsystem of a two-stage system that generates alkyl ester. The first subsystem receives a first reagent, a second reagent and an inert solvent, and passes a mixture that includes the first reaction, the first reagent and the inert solvent through the cartridge, the enzyme facilitates a reaction between the first and second reagent for generating a first product, in which the first product is processed by means of a separator to generate a crude product having a first percentage of alkyl ester. The second subsystem receives the raw product and second additional reagent and generates a second product, in which the second product is processed by means of a second separator to generate a refined product having a second percentage of alkyl ester that is greater than the first percentage . In general, in another aspect, the invention shows an apparatus that includes a cartridge including an enzyme, the cartridge is configured to be coupled to a second subsystem of a two-stage system that generates alkyl ester. The first subsystem receives a first reagent and a second reagent and generates a crude product having a first alkyl ester percentage. The second subsystem receives the raw product and second additional reagent, passes a mixture that includes the raw product and the second additional reagent through the cartridge, the enzyme facilitates a reaction between the components in the raw product and the second reagent to generate an exit , in which the outlet is processed by means of a separation unit to generate a refined product having a second percentage of alkyl ester that is greater than the first percentage. In general, in another aspect, the invention shows an apparatus that includes a cartridge including a lipase, the cartridge being configured to be coupled to an alkyl ester generator. The alkyl ester generator includes a mixer for mixing an oil source and a primary alcohol or a secondary alcohol in an organic solvent to form a solution that is passed through the cartridge, in which the oil source includes a triglyceride and the lipase facilitates a reaction between the triglyceride and the primary alcohol or secondary alcohol to generate an alkyl ester, in which the solution does not undergo phase separation throughout the reaction and the glycerol is produced as a by-product. The alkyl ester generator also includes an evaporator for removing the organic solvent and the unreacted primary alcohol or secondary alcohol, a phase separator for separating the alkyl ester from the glycerol, and a second separator for separating the alkyl ester from the oil source without reacting The implementations of the invention could include one or more of the following features. The second separator includes a short path evaporator. In general, in another aspect, the invention shows an apparatus that includes a cartridge including a lipase, the cartridge being configured to be coupled to an alkyl ester generator. The alkyl ester generator includes a mixer for mixing an oil source and a primary alcohol or a secondary alcohol in an organic solvent to form a solution that is passed through the cartridge, in which the oil source includes a carboxylic acid and the lipase facilitates a reaction between the carboxylic acid and the primary alcohol or secondary alcohol to generate an alkyl ester, in which the solution does not undergo phase separation throughout the reaction and water is produced as a by-product. The alkyl ester generator also includes an evaporator for removing the organic solvent and the unreacted primary alcohol or secondary alcohol and a separator for separating the alkyl ester from the unreacted oil source. The implementations of the invention could include one more of the following features. The separator includes a short path evaporator. In general, in another aspect, the invention shows an apparatus that includes an evaporator having an inlet for receiving a mixture including alkyl ester, alcohol, an inert solvent and glycerol, the evaporator for evaporating the inert solvent and the alcohol to generate a solution including alkyl ester and glycerol, and a separator having an inlet to receive the solution, the separator for separating the alkyl ester from the glycerol based on the liquid-liquid phase separation. In general, in another aspect, the invention shows an energy generator that includes an alkyl ester generator based on enzyme and an electricity generator. The alkyl ester generator includes an inlet for receiving a mixture that includes reagents, an enzyme for facilitating a reaction between the reactants to generate alkyl ester, and a regeneration mechanism for sending at least a portion of the alkyl ester from the exit back to the entry. The generator of electricity that includes an input to receive the alkyl ester generated by means of the alkyl ester generator, a converter to convert energy in the alkyl ester into electricity and an output to produce the electricity generated by the converter. The implementations of the invention could include one or more of the following features. At least a portion of the alkyl ester generator is driven by the electricity generated by the electricity generator. Reagents include triglyceride and alcohol. In general, in another aspect, the invention shows a vehicle that includes a reservoir for storing the reagents; an alkyl ester generator based on enzyme and a motor. The alkyl ester generator includes an inlet to receive a mixture that includes the reagents, an enzyme to facilitate a reaction between the reactants to generate alkyl ester, and a regeneration mechanism to send at least a portion of the alkyl ester from the exit back to the entrance. The motor includes an inlet for receiving the alkyl ester generated by the alkyl ester generator, and a converter for converting the energy in the alkyl ester to kinetic energy. The implementations of the invention could include one or more of the following features. At least a portion of the alkyl ester generator is driven by the kinetic energy generated by the engine. In some examples, the vehicle also includes transmission mechanism for transmitting kinetic energy to wheels. In some examples, the vehicle also includes transmission mechanism to transmit the kinetic energy to the propellers. In general, in another aspect, the invention shows a vehicle that includes a reservoir for storing reagents, an alkyl ester generator based on enzyme and an electricity generator. The alkyl ester generator includes an inlet to receive a mixture that includes the reagents, an enzyme to facilitate a reaction between the reagents to generate alkyl ester, and a regeneration mechanism to send at least a portion of the alkyl ester from the return outlet. at the entrance. The electricity generator includes an inlet for receiving the alkyl ester generated by the alkyl ester generator, a converter for converting energy in the alkyl ester to electricity, and an output for producing the electricity generated by the converter. The vehicle also includes electronic components and power lines to transmit at least a portion of the electricity generated by the electricity generator to the electronic components. The implementations of the invention could include one or more of the following features. In some examples, the vehicle includes an airplane. In some examples, the vehicle includes a car.

In some examples, the vehicle includes a ship. In general, in another aspect, the invention shows a construction that includes a kitchen for processing food; a warehouse to store recycled oil in food processing; and an alkyl ester generator based on enzyme. The alkyl ester generator includes an inlet to receive a mixture including recycled oil and a reagent, an enzyme to facilitate a reaction between the recycled oil and the reagent to generate alkyl ester and a regeneration mechanism to send at least a portion of the ester I rent from the exit back to the entrance. The implementations of the invention could include one or more of the following features. The construction also includes an electricity generator that includes an input to receive the alkyl ester generated by the alkyl ester generator, a converter to convert energy into the alkyl ester into electricity, and an output to produce the electricity generated by the converter; and power lines to transmit at least a portion of the electricity for construction. In general, in another aspect, the invention shows an apparatus for producing alkyl ester, the apparatus includes a mixer for mixing an oil source and a primary alcohol or secondary alcohol in an organic solvent to form a solution, the source of oil including a triglyceride; a reactor for receiving the solution, the reactor including a lipase which facilitates a reaction between the triglyceride and the primary alcohol or the secondary alcohol to generate an alkyl ester, in which glycerol is produced as a by-product; an evaporator to remove the organic solvent and unreacted primary alcohol or secondary alcohol; and a phase separator for separating the alkyl ester from the glycerol. The implementations of the invention could include one or more of the following features. The solution received by the reactor does not undergo phase separation throughout the reaction. Each molecule of the organic solvent includes a number of carbon atoms and a heteroatom, in which the number ranges from 4 to 8. The organic solvent includes a C4 to C8 tertiary alcohol. The organic solvent includes at least one of f-butanol, 2-methyl-2-butanol, 2,3-dimethyl-2-butanol, 2-methyl-2-pentanol, 3-methyl-3-pentanol, 3-ethyl- 3-pentanol, 2,3-dimethyl-2-pentanol, 2,3-dimethyl-3-pentanol, 2,2,3-trimethyl-3-pentanol, 2-methyl-2-hexanol and 3-methyl-3- hexanol. The organic solvent includes pyridine. At least one of the primary alcohols and the secondary alcohol consists of 1 to 18 carbon atoms. The source of oil includes at least one plant oil, animal oil and useless fat. The apparatus also includes a vehicle, in which the lipase is immobilized in the vehicle. The lipase includes at least one Antarctic candida lipase, thermomyces lanuginosa limuna, lapase pseudomonas fluorescens, pseudomonas lipase cepacia and chromobacterium viscosum lipase. A portion of the reactor is maintained at a reaction temperature of 0 to 95 ° C to facilitate the reaction between the triglyceride and the primary alcohol or the secondary alcohol. The apparatus also includes a pump configured to cause the solution to flow through the reactor from 1 to 180 minutes. The apparatus also includes a heater to heat the oil source to a range of 150 to 215 ° C. The hot oil source is cooled to the reaction temperature before the source of oil is sent to the mixer. The apparatus also includes an inlet for adding an alkyl ester to the solution before the solution is sent to the reactor. The apparatus also includes a return mechanism to allow at least a portion of the alkyl ester to be separated by means of the phase separator to enter it at the inlet and add it to the solution. In general, in another aspect, the invention shows a method that includes inserting a cartridge into an alkyl ester generator, the cartridge having an inlet and outlet, and an enzyme placed between the inlet and the outlet; read information encoded in the cartridge; control an operation of the alkyl ester generator based on the information. The implementations of the invention could include one or more of the following features. Controlling an operation of the alkyl ester generator includes controlling at least one of temperature and flow rates of a solution floating on the cartridge inlet.

In general, in another aspect, the invention shows a method for processing food, the method includes processing food using oil; recycle the oil used to process the food; receive a mixture that includes recycled oil, a reagent and an inert solvent; use enzyme to facilitate a reaction between the recycled oil and the reagent to generate alkyl ester; recycling at least a portion of the alkyl ester by mixing at least a portion of the alkyl ester with the mixture, the alkyl ester assisting in the dissolution of the recycled oil and the reagent; generate electricity or kinetic energy of the alkyl ester; and energy devices used to process food, using electricity or kinetic energy. In general, in another aspect, the invention shows a method for operating a vehicle, the method including receiving a mixture including reagents and an inert solvent, passing the mixture through an enzyme cartridge to facilitate a reaction between the reagents to generate alkyl ester; recycling at least a portion of the alkyl ester by mixing at least a portion of the alkyl ester with the mixture, the alkyl ester assisting in the dissolution of the reactants; generate electricity or kinetic energy of the alkyl ester; and energy devices used to operate the vehicle using electricity or kinetic energy. Other features and advantages of the invention are apparent from the following description of the claims. All publications, patent applications, patents or other references mentioned are incorporated for reference. In case of conflict with the references incorporated for reference, the present specification, including the definitions, will be controlled.

DESCRIPTION OF THE DRAWINGS FIG. 1 is a block diagram of a fuel production system. FIGS. 2A-2D are block diagrams of different configurations of a fuel production plant. FIG. 2A is a simple stage plant with regeneration of crude bio-diesel. FIG. 2B is a two-stage plant with regeneration of crude bio-diesel from the first stage. FIG. 2C is a single-stage plant. FIG. 2D is a two-stage plant. FIG. 3 is a block diagram of a single-stage plant with regeneration of crude bio-diesel. FIG. 4 is a schematic diagram of a single-stage plant with regeneration of crude bio-diesel. FIGS. 4A-C are elongated views of portions of FIG. 4. FIG. 5 is a schematic diagram of a single-stage plant with regeneration of crude bio-diesel. The FiGS. 5A-D are elongated views of portions of FIG. 5. FIG. 6 is a schematic diagram of a two-stage plant with regeneration of crude bio-diesel. FIGS. 6A-C are elongated views of portions of FIG. 6 FIG. 7 is a block diagram of the fuel production system. FIG. 8 is a block diagram of a fuel production system coupled to an electric generator. FIG. 9 is a block diagram of a vehicle that has a fuel production system. FIG. 10 is a block diagram of a fuel production system coupled to a fuel processing unit.

DESCRIPTION 1 General Perspective Referring to FIG. 1, a fuel production system includes a processing plant 100 that takes a 1 10 oil source, such as soybean oil and produces a bio-diesel fuel 150, such as alkyl ester or a related product such as lubricating oil or a chemical intermediate The processing plant 1 00 uses one or more reactors 140, each using an enzymatic catalyst 142. The processing plant uses an inert solvent 120, such as a tertiary alcohol anhydride or anhydrous pyridine, as well as a reagent 130, such as a primary alcohol or secondary such as methanol anhydride. During processing, the processing plant 1 00 recovers some of the inert solvent 120 and reagent 130 to fill the supply. The processing plant also produces co-products 160, such as waste water or glycerol.

A number of different versions of the processing plant are described below. These versions differ, for example, in features such as the number of reactor processing stages (for example, single stage with a reactor, two stages with two reactors), regeneration arrangements of intermediate crude bio-diesel for reactor reactors of the reactor. previous stage and in the particular oil source, inert solvent, reactant, biocatalysts and associated operating conditions used. For example, the processing plant may operate in a continuous flow mode or alternatively in a batch mode. Different versions of the processing plant could have different physical sizes. In one example, the plant is relatively compact, for example, the size of a refrigerator, allowing deployment at the point where bio-diesel fuel is consumed, such as at the location of a diesel engine used for generating electricity. Other versions could be significantly larger with corresponding higher production capacity. In some examples, the plant can be designed for home use, has sizes that are similar to a large refrigerator and can have a production capacity of 200 liters per day or less. In other examples, the plant can be designed for farm, alley or military field use and has a similar size to containers that have a length in a range of 51 to 102 centimeters. In other examples, plant 100 can be designed for a commercial plant that has a capacity that extends from 40,000 tons to more than 25,000 tons annually. 1 .1 Plant Configurations Referring to FIGS. 2A-D, four example configurations make use of different numbers of stages and different types of regeneration. Referring to FIG. 2A, a single stage plant utilizes a single reactor 140. The reactor outlet (R-1) 140 is fed to a separator (S-1) 220, which includes components for separating the inert solvent 120, unreacted reactant 130. and by-products 160 from the reactor outlet to produce a crude bio-diesel product 225, for example, using a combination of an evaporator or a liquid-liquid separator. The reactor inlet R-1 140 is supplied from the outlet of a mixer 210, which accepts the oil source 1 10, the inert solvent 120 and the reagent 130. In this version of the plant, the mixer 210 also receives something of the raw bio-diesel 225 available from the outlet of separator S-1. This regeneration of the crude bio-diesel has two advantages: (1) it enhances the completeness of the reaction between the reactants and (2) it reduces the amount of inert solvent required to combine in the mixer 21 0. The outlet of the separator 220 is fed to a final separator 230, for example, a short path evaporator or a short path distillation, which also purifies the bio-diesel to produce the output of "pure" bio-diesel 150. As an example, the raw bio-diesel 225 could be 90-99% pure by weight and 150 pure bio-diesel could be greater than 99% pure by weight. This version of the plant has relatively few components which is therefore appropriate for small and portable versions, as well as larger versions. Referring to FIG. 2B, a two-stage plant 100B uses the two stages 101 and 105, each one including a reactor 140. The arrangement of a first reactor (R-1) 140 and a first separator (S-1) 220 is similar to that shown in FIG. 2A, including using a regeneration of raw bio-diesel 225 from the outlet of the first separator 220 to the mixer 210 for the first reactor 140. In this version of the plant, the outlet of the first separator 220 is fed to a second mixer 210 which combines the crude bio-diesel 225 with additional inert solvent 120 and reagent 130. The outlet of the second mixer 210 is fed to a second reactor (R-2) 140. The outlet of the second reactor 140 is passed through a second separator (S -2) 220. The output of the second separator 220 can be used directly as the bio-diesel fuel 150, or preferably passed through a final separator 230 before the exit. As an example, in such a two-stage plant, the raw bio-diesel output 225 from the first separator 220 is at least 90% pure by weight, while the outlet of the second separator is at least 95% pure. Referring to FIGS. 2C-D, plants that do not use the regeneration of the crude bio-diesel have configurations that are otherwise similar to the plants shown in FIGS. 2A-B, respectively. As examples, the outputs of the first separators 220 in these versions of the plant are at least 80% pure, and in the two-stage version shown in FIG. 2D, the output of the second separator is at least 95% pure. The single stage plant 100C is useful, for example, when the catalyst (such as a particular type of lipase) is expensive and the final product has high added value, such as for medical or drug use. The amount of lipase that is required in the 100C single stage plant could be less than that of the double stage 100B and 100D plants, and therefore the final product can be produced with more cost efficiency. The plants 100A to 100D can have various configurations. Additional components could be included in the plants, such as heat exchangers to increase or decrease the temperatures of the solutions and pumps to control the flow of the solutions. Disposal beds could be included to remove unwanted moisture, glycerol or other unwanted impurities from the products. For example, in the single-stage plant 100C, the separator 220 can separate unreacted raw material completely (eg reagent and oil source) from the product, so that the unreacted raw material can be completely recrystallized. In this case, a glycerol removal bed, filled with ion exchange resin, can be used to remove traces of glycerol from the recycled raw material. In some examples, when certain types of enzymatic catalysts are used, for example, lipase thermomyces lanuginosa, it is useful to limit the amount of moisture in the solution flowing in reactor 140. In such cases, a bed of water elimination of the cartridge type Filled with moisture absorbing resin (or absorption), it can be used in the oil regeneration inlet flow for smaller plants. For larger plants, water moisture can be controlled by other disposal techniques, such as evaporating or separating hot dry air. In some examples of the two-stage plants (e.g., 100B and 100D), the final separator 230 may be omitted. In plants 100A to 100D, the equilibrium of the reaction in the reactors 140 can be determined by means of thermodynamics and is independent of the type of enzymatic catalyst used. Therefore, the bio-diesel concentration at equilibrium is a function of temperature, inert solvent concentration, reagent concentrations and product concentrations. Different equilibrium concentrations of the bio-diesel can be obtained at different temperatures when the conditions remain the same. 1 .2 Chemical Configurations A variety of combinations of oil sources, inert solvents, reactants and catalysts associated operating conditions, including temperature and reaction times, appropriate for the fuel production plant versions are described in the Application for USA No. 10 / 945,339, registered on September 20, 2004, entitled "Métpdos to Produce Esres Alquilo," for Chih-Chung Chou, which is incorporated for reference. The processing proposal is based on the discovery that high purity alkyl esters can easily be produced from an oil regeneration (eg, vegetable oils or animal fats) by a catalyzed lipase reaction, in which the inactivity of lipases is minimized. In particular, an alkyl ester can be produced, for example, by a trans-esterification or esterification reaction. The method includes (1) mixing an oil source containing a triglyceride or a carboxylic acid and a first primary alcohol or a first secondary alcohol in a first organic solvent to form a first solution; wherein each molecule of the first organic solvent contains 4-8 carbon atoms and a heteroatom; (2) reacting the triglyceride or the carboxylic acid with the first primary alcohol or the first secondary alcohol in the presence of a first lipase to produce a first alkyl ester, in which the first solution does not undergo phase separation throughout the reaction; and (3) separating the first alkyl ester from the first solution. Examples of an appropriate oil source include plant oil (e.g., microalgae oil), animal oilof. (eg, fish oil, lard, melted fats or tallow), waste fat (eg, restaurant waste grease), or a hydrolytic fraction thereof (eg, carboxylic acid). Before the mixing stage, the oil source can be heated to 150-215 ° C and cooled to reaction temperature. Prior to the reaction, the oil source can be mixed with the first primary alcohol or the first secondary alcohol in the first organic solvent to form a one-phase solution. Examples of the first primary and secondary alcohols include those containing from 1 to 18 carbon atoms, such as methanol, ethanol, isopropanol, isobutanol, 3-methyl-1-butanol, hexanol, octanol, decanol or lauryl alcohol. Examples of the first organic solvent include pyridine or a C4-C8 tertiary alcohol (e.g., t-butanol, 2-methyl-2-butanol, 2,3-dimethyl-2-butanol, 2-methyl-2-pentanol, 3 -methyl-3-pentanol, 3-ethyl-3-pentanol, 2,3-dimethyl-2-pentanol, 2,3-dimethyl-3-pentanol, 2,2,3-trimethyl-3-pentanol, 2-methyl -2-hexanol or 3-methyl-3-hexanol). The first organic solvent can also be mixed with other suitable solvents. Preferably, the first organic solvent can be mixed with alkyl ester, which can be an alkyl ester obtained from the method of this invention or an alkyl ester obtained from other sources (eg, purchased from a commercial source). When the first organic solvent is used together with another solvent, it is added in an amount sufficient to maintain the homogeneity of the first solution during the reaction, hence minimizing the inactivity of the first lipase. The term "lipase" refers to any enzyme capable of catalyzing a trans-esterification or esterification reaction. Examples include lipase candida antárctica, lipase thermomyces lanuginosa, lipase pseudomonas fluorescens, lipase pseudomonas cepacia or lipase chromobacterium viscosum. The first lipase may include a single lipase or a combination of two or more lipases. It is preferably immobilized in a vehicle in the first reactor. The trans-esterification or esterification reaction can be carried out at 0-95 ° C (for example 20-95 ° C) for 1 -180 minutes (for example, 10-90 minutes or 20-60 minutes) to obtain the first alkyl ester. During a trans-esterification reaction between an oil source containing a triglyceride and a primary or secondary primary alcohol, glycerol is produced as a by-product. Unexpectedly, the first alkyl ester can be easily obtained by phase separation between the first alkyl ester and the glycerol, after removing the first organic solvent and the first unreacted primary or secondary alcohol by evaporation. The oil source just mentioned could also contain monoglycerides, diglycerides or carboxylic acids. The monoglycerides and the diglycerides react with the first primary or secondary alcohol in a manner similar to the triglyceride. The carboxylic acids react with the first primary or secondary alcohol by means of an esterification reaction, in which the water is produced as a by-product and can be easily removed during the evaporation process. During an esterification reaction between an oil source containing a carboxylic acid and a primary or secondary primary alcohol, water (but without glycerol) is produced as a by-product. It is also unexpected that the first alkyl ester can be easily obtained by removing the first organic solvent, the first unreacted primary or secondary alcohol and the water by evaporation. When the above-mentioned source of oil contains a significant amount of triglycerides, diglocerides or monoglycerides, the first alkyl ester can be obtained in the manner described in the preceding paragraph. If the first alkyl ester obtained above is contaminated with monoglycerides, diglycerides, triglycerides or carboxylic acid, the contaminants can be eliminated by further reacting them with an alcohol by another trans-esterification or esterification reaction. Specifically, the first alkyl ester can be mixed with a second primary alcohol or a second secondary alcohol in a second organic solvent to form a second solution. Each molecule of the second organic solvent contains 4-8 carbon atoms and a heteroatom. The second organic solvent may be the same as or different from the first organic solvent. The second primary or secondary alcohol is preferably equal to the first primary or secondary alcohol. The monoglycerides, diglycerides, triglycerides or carboxylic acid in the second solution can then be reacted with the second primary alcohol or the second secondary alcohol in the presence of a second lipase to produce a second alkyl ester. In the reaction, the second solution does not undergo phase separation. The second lipase may be the same as or different from the first lipase. The first and second alkyl esters obtained in this way can then be separated from the second solution. Preferably, the second alkyl ester is identical to the first alkyl ester. A number of examples of the proposed processing are described below. 1.2. 1 EXAMPLE 1 Soybean oil was used as a source of oil to prepare alkyl esters. Specifically, the refined soybean oil (55.4% p) was mixed with anhydrous methanol (8.6% p) and anhydrous t-butanol (36.0% p) in a first mixer to form a one-phase solution. The solution was then sent to a first reactor, which was filled with NOVOZYM 435 (a lipase candida Antarctica; Novozymes A / S, Bagsvaerd, Denmark). Specifically, NOVOZYM 435 was immobilized in a vehicle (a macro-porous resin) and then placed in the reactor. The reactor temperature was 45 ° C. The reaction time was 62 minutes. After the reaction was complete, the solution was fed to a vacuum evaporator and then to a liquid-liquid separator to obtain a product. The composition of the product was determined by HPLC (column: Luna Su C18 (2) 250x4.6mm, phenomenex, mobile phases: methanol, hexane and isopropanol, UV detector: UV-2075, JASCO, Japan). Unexpectedly, the product obtained contained 96.19% p of alkyl esters, 3.59% p of monoglycerides and diglycerides, and 0.22% p of triglycerides.

In another experiment, an alkyl ester was used as a co-solvent. Specifically, refined soybean oil (49.1% p) was mixed with anhydrous methanol (7.6% p), t-butanol anhydride (20.5% p) and an alkyl ester (22.8% p) in a first mixer to form a solution of a phase. The reaction conditions were the same as those described above, except that the reaction was completed in 58.0 minutes. Unexpectedly, the product obtained contained 96.10% p of alkyl esters, 3.23% p of monoglycerides and diglycerides, and 0.67% p of triglycerides. In a further experiment, t-amyl alcohol and an alkyl ester were used as solvents. Specifically, refined soybean oil (40.8% p) was mixed with anhydrous methanol (6.3% p), t-amyl anhydride alcohol (37.3% p), and an alkyl ester (15.6% p) in a first mixer to form a solution of a phase. The reaction conditions were the same as those described above, except that the reaction was completed in 53.0 minutes. Unexpectedly, the product obtained contained 96.96% p of alkyl esters, 2.64% p of monoglycerides and diglycerides, and 0.40% p of triglycerides. 1.2.2 Example 2 An alkyl ester of Example 1 was mixed with anhydrous methanol and anhydrous t-butanol in another mixer to form a one-phase solution. The solution in this formed manner contained 70.00% p of the alkyl ester, 2.8% p of contaminants (ie, 2.47% p of monoglycerides and diglycerides and 0.31% p of triglycerides), 7.28% p of the methanol and 19.94% p of the t- butanol. The solution was then sent to another reactor, which was filled with NOVOZYM 435. Specifically, NOVOZYM 435 was immobilized in a vehicle and then placed in the reactor. The temperature of the second reactor was 45 ° C. The reaction time was 17.5 minutes. After the reaction was complete, the solution was fed to another vacuum evaporator and then to another liquid-liquid separator to obtain a product. The composition of the product was determined by HPLC. Unexpectedly, the product obtained above contained 99.24% p of alkyl esters, 0.65% p of monoglycerides and diglycerides, and 0.1 1% p of triglycerides. 1.2.3 Example 3 Other sources of oil, in addition to soybean oil, were used as starting materials for preparing alkyl esters in a manner similar to that described in Example 1. The sources of oil used included restaurant waste fats containing high free fatty acids, restaurant waste fats containing low free fatty acids, tallow, lard, fish oil, palm oil and castor oil. In one experiment, restaurant waste fat, containing high free fatty acids, was used. Specifically, the reactor containing NOVOZYM 435 was fed with a solution containing a solution of said restaurant waste grease (49.1% p), anhydrous methanol (7.6% p), t-butanol (20.5% p) and an alkyl ester (22.8% p). % p). Specifically, NOVOZYM 435 was immobilized in a vehicle and then placed in the reactor. The temperature of the reactor was 45 ° C. The reaction time was 24.0 minutes. The product of the reactor was isolated and its composition was determined by HPLC. Unexpectedly, the product obtained above contained 96.63% p of alkyl esters, 3.17% p of monoglycerides and diglycerides, and 0.20% p of triglycerides. In another experiment, fish oil (an animal oil) was used as a source of oil. Specifically, the fish oil (52.4% p) was mixed with anhydrous methanol (7.8% p) and anhydrous pyridine (39.8% p) in a first mixer to form a one-phase solution. The reaction conditions were the same as those described above, except that the reaction was completed in 25.0 minutes. Unexpectedly, the product obtained contained 95.63% p of alkyl esters, 3.03% p of monoglycerides and diglycerides, and 1.34% p of triglycerides. In another additional experiment, palm oil (a plant oil) was used as a source of oil. Specifically, the oil of plants (46.5% p) was mixed with anhydrous methanol (7.5% p) and t-amyl alcohol anhydride (46.0% p) in a first mixer to form a one-phase solution. The reaction conditions were the same as those described above, except that the reaction was completed in 41.0 minutes. Unexpectedly, the product obtained contained 96.97% p of alkyl esters, 1.95% p of monoglycerides and diglycerides, and 1.08% p of triglycerides. 1.2.4 Example 4 Primary alcohols were used as starting materials for preparing alkyl esters in a manner similar to that described in Example 1. The alcohols used included methanol, ethanol, isobutanol, 3-methyl-1-butanol, hexanol, octanol, decanol and lauryl alcohol. In one experiment, the reactor containing NOVOZYM 435 was fed with a solution containing fish oil (52.0% p), ethanol (11.2% p), and t-butanol anhydride (36.8% p). Specifically, NOVOZYM 435 was immobilized in a vehicle and then placed in the reactor. The temperature of the reactor was 45 ° C. The reaction time was 39.0 minutes. The reactor product was isolated and its composition determined by HPLC. Unexpectedly, the product obtained above contained 97.44% p of alkyl esters, 1.44% p of monoglycerides and diglycerides and 1.1% p of triglycerides. In another experiment, hexanol (a C6 alcohol) was used as a starting material. Specifically, soybean oil (53.7% w) was mixed with anhydrous hexanol (26.6% wt) and anhydrous t-butanol (19.7% wt) in a first mixer to form a one-phase solution. The reaction conditions were the same as those described above, except that the reaction was completed in 46.0 minutes. Unexpectedly, the product obtained contained 95.06% p of alkyl esters, 4.1 1% p of monoglycerides and diglycerides and 0.88% p of triglycerides. In still another experiment, lauryl alcohol (a C 12 alcohol) was used as a starting material. Specifically, soybean oil (37.2% w) was mixed with lauryl alcohol anhydride (33.6% wt) and t-butanol anhydride (29.2% wt) in a first mixer to form a one-phase solution. The reaction conditions were the same as those described above, except that the reaction was completed in 66.0 minutes. Unexpectedly, the product obtained contained 95.03% p of alkyl esters, 4.07% p of monoglycerides and diglycerides, and 0.90% p of triglycerides. 1.2.5 Example 5 Secondary alcohols were used as starting materials for preparing alkyl esters in a manner similar to that described in Example 1. The alcohols used included isopropanol (a C3 alcohol), 2-butanol (a C4 alcohol) and secondary n-octyl alcohol (a C8 alcohol). In one experiment, the reactor containing NOVOZYM 435 was fed with a solution containing wild turnip oil (52.9% p), sopropanol (14.1% p) and t-amyl anhydride alcohol (33.0% p). Specifically, NOVOZYM 435 was immobilized in a vehicle and then placed in the reactor. The temperature of the reactor was 45 ° C. The reaction time was 39.0 minutes. The product of the reactor was isolated and its composition was determined by HPLC. Unexpectedly, the product obtained above contained 93.92% p of alkyl esters, 4.86% p of monoglycerides and diglycerides, and 1.22% p of triglycerides. In another experiment, 2-butanoI was used as a starting material. Specifically, soybean oil (52.5% w) was mixed with 2-butanol anhydride (18.9% wt) and t-amyl alcohol anhydride (28.6% wt) in a first mixer to form a one-phase solution. The reaction conditions were the same as those described above, except that the reaction was completed in 46.0 minutes. Unexpectedly, the product obtained contained 92.84% p of alkyl esters, 5.08% p of monoglycerides and diglycerides and 2.09% p of triglycerides. In another additional experiment, secondary n-octyl alcohol was used as a starting material. Specifically, soybean oil (46.4% p) was mixed with n-octyl secondary alcohol anhydride (29.3% p) and alcohol t-butanol anhydride (24.3% p) in a first mixer to form a one-phase solution. The reaction conditions were the same as those described above, except that the reaction was completed in 42.0 minutes. Unexpectedly, the product obtained contained 94.69% p of alkyl esters, 2.45% p of monoglycerides and diglycerides, and 2.86% p of triglycerides. 1.2.6 Example 6 An alkyl ester was prepared using lauric acid and methanol as starting materials by means of an esterification reaction in a manner similar to that described in Example 1. Specifically, the reactor containing NOVOZYM 435 was fed with a solution containing lauric acid anhydride (77.7% p), anhydrous methanol (17.6% p) and t-butanol anhydride (4.7% p). The NOVOZYM 435 was immobilized in a vehicle and then in the reactor. The temperature of the reactor was 45 ° C. The reaction time was 37.0 minutes. The product of the reactor was isolated and its composition was determined by GC (8610C, SRI, USA; column: MXT-65TG, length: 30 m, I.D .: 0.25 μm; vehicle gas: He, flow rate: 1 ml / min; injector: division ratio: 20 to 1, temperature: 300 ° C; detector: FID, temperature: 370 ° C). Unexpectedly, the product obtained above contained 96.0% p of methyl laurate and 4.0% p of lauric acid. 1.2.7 Example 7 The alkyl esters were prepared using soybean oil and methanol as starting materials in a manner similar to that described in Example 1, except the soybean oil was heated for a period of time before use. Specifically, the soybean oil was first heated at 200 ° C for 5 minutes or at 210 ° C for 1 hour and then cooled to reaction temperature. Subsequently, the soybean oil (49.1% p) was mixed with anhydrous methanol (7.6% p), t-butanol anhydride (20.5% p) and an alkyl ester (22.8% p) in the blender to form a one-phase solution . The solution was then sent to the reactor, which was filled with NOVOZYM 435. Specifically, NOVOZYM 435 was immobilized in a vehicle and placed in the reactor in advance. The temperature of the reactor was 45 ° C. Each reactor product was isolated and its composition was determined by HPLC. Unexpectedly, it took 50.3 minutes and 47.4 minutes to obtain a product containing less than 1.5% p of triglycerides, using soybean oil heated at 200 ° C for 5 minutes and using soybean oil heated at 210 ° C for 1 hour, respectively. In comparison, it took 53.8 minutes to do it in a similar reaction condition using soybean oil without heat treatment. 1.2.8 Example 8 LIPOZYME TL IM (a thermomyces lanuginosa lipase, Novozymes A / S, Bagsvaerd, Denmark) was used as a catalyst to prepare alkyl esters in a manner similar to that described in Example 1. Specifically, it was immobilized on a granulated silica vehicle and then placed in the reactor. The reactor was then fed with a solution containing soybean oil (49.1% p), anhydrous methanol (7.6% p), t-butanol anhydride (20.5% p) and an alkyl ester (22.8% p). The temperature of the reactor was 45 ° C. The reaction time was 51.0 minutes. The product of the reactor was isolated and its composition was determined by HPLC. Unexpectedly, the product obtained above contained 94. 04% p of alkyl esters, 3.65% p of monoglycerides and diglycerides, and 2.31% p of triglycerides. 2 Proposed production of single-stage bio-diesel fuel Referring to FIG. 3, an example of the processing plant 1 00A of the configuration shown in FIG. 2A includes a number of components used to implement the separators 220 and 230, as well as additional components that are not shown in FIG. 2A used to process the recovered waste and disposal products produced by the separators. In this example, reagent 130 includes an alcohol.

The reactor 140 may be, for example, a plug flow reactor which includes the enzyme catalyst 142. A description of the reaction between the oil source 1 10 and the reactive alcohol 130 can be found in section 1.2. in U.S. Patent Application Ser. 10 / 945,339. The speed of fluid flow through the reactor 140 is controlled so as to satisfy a specified residence time for the reactor 140, allowing sufficient time for the reactions to be completed. The residence time can vary from, for example, 3 hours to less than 20 minutes. The temperature of the reactor 140 is maintained at a predetermined value, which may range from, for example, 20 ° C to 95 ° C, depending, in part, on the type of oil source, reagent and catalyst. The reactor 140 produces a crude product 103, which includes alkyl ester, glycerol and impurities, such as incompletely reacted oils that are generated from the reaction between the oil source 10 and the reagent 1 30. Examples of incompletely reacted oils include monoglycerides and diglycerides. The processing plant 100A includes a separation module 220 which separates the raw product components 103 in, for example, crude oil 168 and crude bio-diesel 150, including unreacted oil 1 10, inert solvent 120 and unreacted reagent 130. separation module 220 includes a vacuum evaporator, such as a clean thin layer evaporator 324, model type VD, made by Verfahrens Technische Aulagen GmbH, Deggendorf, Germany, or a single flash drum integrated with a packed bed evaporator. The thin membrane evaporator 324 separates the various components in the crude product 103 using thin membrane evaporation. The thin membrane evaporator 324 includes a thin membrane having a large surface area, so that the inert solvent 120, the unreacted alcohol 130 and the water can evaporate at a faster rate. Components having lower boiling points, such as unreacted alcohol 130, water vapor, inert solvent and other impurities, flash, condense and collect in a solvent recovery unit 328, which separates the inert solvent 120, the unreacted alcohol 130, the water vapor and other impurities. The inert solvent 120 and unreacted alcohol 130 can be recycled and mixed with fresh solvent 120, fresh oil source 1 10 and fresh reactive alcohol 130 as part of the inlet to reactor 140. Water vapor and other impurities are sent to a catalyst converter 362, which converts the impurities into, for example, carbon dioxide. Water vapor and carbon dioxide are removed through a vent (not shown). The residue of the thin membrane evaporator 324 includes glycerol, alkyl ester, unreacted oil and incompletely reacted oil, which are sent to a first agglutinator and separator 336. The binder agglutinates the glycerol drops in liquid form. After the solution settles for a period of time in the separator, the bio-diesel and glycerol will separate, forming an upper layer of bio-diesel and a lower layer of glycerol. The lower glycerol layer is referred to as crude glycerol 168, which includes impurities, such as water, inert solvent and unreacted alcohol. The crude glycerol 168 is sent to a crude glycerol evaporator 338. An example of the evaporator 338 is a short path evaporator, such as the type VK model, made by VTA GmbH, or a flash drum coupled with a packed bed evaporator. The evaporator 338 operates by means of evaporation to separate the glycerol from the impurities and removes the "pure" glycerol 14. As an example, the pure glycerol 14 may be at least 99% pure by weight. The upper layer of the bio-diesel is referred to as the crude bio-diesel 225 because it includes impurities, such as incompletely reacted oil, unreacted oil and a trace amount of glycerol. A portion of the crude bio-diesel 225 is recycled and fed back into the reactor 140. As described above, recycling the crude bio-diesel 225 can reduce the amount of inert solvent that is required to dissolve the oil source and the reactive alcohol, in addition to the advantage of promoting the completion of the reaction. The portion of the crude bio-diesel 225 that is not recycled is sent to the final separator 230, which includes a short path evaporator 344 that separates the bio-diesel from the impurities to generate the pure bio-diesel 150. The path evaporator cut 344 produces incomplete oil, unreacted oil and glycerol to a second agglutinator and separator 354 or to a bed of ion exchange resin that is regenerated (plug flow bed), which separates or removes glycerol from the other components. The binder and separator 354 produces crude glycerol 156 for the crude glycerol evaporator 338, which processes the crude glycerol 156 to generate crude glycerol 1 14. The binder and separator 354 produces incomplete and unreacted oils, which optionally are they can recycle and feed back to reactor 140. 3. Detailed design of a simple stage system Referring to FIG. 4, another example of the plant 110A of the configuration shown in FIG. 2A is described in detail below. Referring to FIG. 4, plant 1 10A includes an oil drum (D-1) which stores the oil source 1 10. The inert solvent 120 is stored in a solvent drum, which receives fresh inert solvent, inert solvent recycled from the unit of solvent recovery inside the plant and nitrogen gas. Nitrogen gas blocks the moisture and oxygen of the solvent. Reactive alcohol 130 is stored in a reagent alcohol drum, which receives fresh reactive alcohol, recycled reactive alcohol and nitrogen gas. The mixture of the oil source 1 10, inert solvent 120 and reactive alcohol 130 is made using a number of components. A two-way metering pump (P-1) 430 pumps the oil source 1 10 together with a path 432 at a fixed rate to a water removal bed (RB-1) 436, which may be, for example , a packed bed, filled with superabsorbent polymer that removes traces of water directly from the oil source. After the water is removed, the oil source is sent through a pipe 440 to the mixer 210, which includes a static mixer (SM-1) 438. At the same time, a two-way metering pump (P-2) 424 pumps the reagent and the inert solvent to the static mixer 438 at a rate so that the oil source ratio versus the reactive alcohol and the inert solvent is maintained at a predetermined value. The pump 430 also pumps recycled raw bio-diesel 225 through a pipe 476 to the static mixer 438, at a predetermined ratio of recycled crude bio-diesel versus oil source. The static mixer 438 may be, for example, a multi-element static mixer such as described in US Pat. UU No. 3,286,992, or a compact mixer, such as the Sulzer Compact Static Mixer, available from Sulzer Chemtech, Switzerland. A static mixer has no moving parts, and mixes the solution without external power. The static mixer 438 causes the reagent, the inert solvent, the oil source and the recycled crude bio-diesel to mix thoroughly to produce a homogeneous solution. The reactor 140, which includes a heat exchanger (HE-1) 448 and a reactor of the cartridge type (R-1) 404, receives the production of the mixer 210. Specifically, the production of the static mixer 438 is forwarded to the heat exchanger (HE -1) 448, which regulates the temperature of the mixed solution through the use of, for example, cooling water, hot oil, steam or electric heaters or refrigerators. The heat exchanger 448 may have, for example, a double pipe design. The solution is then introduced into an elongate cartridge 404 of the reactor which is filled with enzyme catalyst 142, in this case lipase. The reaction temperature may be in the range of 0 to 95 ° C, preferably at room temperature (for example 25 ° C). A number of alternative types of cartridge 404 may be used. For example, the cartridge 404 may be a column with the aid of a grid in the bottom. A screen is provided at the bottom of the cartridge to retain the enzymatic catalyst 142 within the cartridge and another screen is supplied in the upper portion of the cartridge to level a flow of the solution in the cartridge. Between the two screens, the cartridge is filled with the catalyst. The mixed temperature regulated solution enters the cartridge 404 through an opening in the top of the cartridge and flows down through the enzymatic catalyst 142. The enzymatic catalyst facilitates a reaction between the reactive alcohols and the oil source, which includes triglyceride to generate alkyl ester, glycerol, and water (and / or other impurities). Reactor 140 produces a crude product which includes alkyl ester, glycerol, unreacted oil (triglyceride), incomplete oil (monoglycetide and diglyceride), unreacted alcohol, inert solvent and other impurities. As described above with reference to FIG. 3, the crude production of the reactor 140 is passed to a separator 220, which includes an evaporator 324 and a binder and separator 336. In FIG. 4, a particular design of the binder and separator 336 is indicated by reference numeral 336A, in which a membrane filter with a pore size of 1-5 μm is used to bind the glycerol drops. In the plant 1 10A shown in FIG. 4, the evaporator 324 includes a pressure regulator (PR) 452, a preheater (HE-2) 448 and an integrated single scintillator drum evaporator with a packed bed design (E-1) 451. The preheater 448 can use, for example, hot oil or steam to pre-heat the raw product. The evaporator 451 may use hot oil or steam as a heating medium in the chamfered area. Within the evaporator 451, inert solvent, water and unreacted alcohol are evaporated and exit the evaporator 451 through a top opening. The inert solvent, the water and the unreacted alcohol are condensed and collected in the solvent recovery unit 328 (not shown in FIG 4) and can be recycled. The composition of the compensated liquid in the solvent recovery unit could include unreacted alcohol, inert solvent, water and trace amounts of bio-diesel. Two simple columns can be used to separate unreacted alcohol, inert solvent and water. In one example, the first column separates the inert solvent from the unreacted alcohol and water. The inert solvent, including trace amounts of the bio-diesel, if any, exits from the bottom of the first column and is recycled to the inert solvent drum. In the solvent recovery unit, the unreacted alcohol and water come out from the top of the first column and sent to the second column, where the unreacted alcohol is collected in an upper reflux drum and recycled to the reagent alcohol drum. The bottom residue in the second column consists mostly of water and small amounts of unreacted alcohol and inert solvent. The small amount of unreacted alcohol and the inert solvent can be vaporized through a catalyst converter and burned completely. Both simple columns can be operated automatically at ambient pressure. In general, the design of solvent recovery depends on the alcohol and inert solvent used and the different recovery schemes that could be used. Continuing with FIG. 4, the components in the evaporator 451 that have higher boiling points are pumped to a gear pump (p-6) for a binder (CL-1) 454, and the glycerol drops are agglutinated in large droplets that can be Easily separate from the raw bio-diesel. Two liquids are formed in the liquid-liquid phase separator (S-2) 456. The raw bio-diesel is sent through the refrigerant (HE-3) 458 and a tracer bed of glycerol (RB-3) 461, which is filled with ion exchange resin that can be regenerated. The exit of the trace removal bed of glycerol 461 is displayed in two streams 476 and 478. One stream 476 is recycled to the static mixer 438, the other stream 478 is sent to the short path evaporator (E-2) 424. Crude biodiesel, which could include at least 95% by weight of alkyl ester, flows out of separator 456 and is cooled by means of the refrigerant (HE-3) 458. Coolant water is used to cool the crude bio-diesel in the refrigerant . A portion of the raw bio-diesel is recycled through a 476 regeneration pipeline. The recycled raw bio-diesel passes a 478 triple-pass solenoid valve, which can be switched between raw bio-diesel and pure bio-diesel. As described above, the pump 430 pumps the recycled bio-diesel to the static mixer 438. The portion of the green bio-diesel that is recycled is sent to the short path evaporator 344 (part of the final separator 230 as shown in FIG. . 3). The short path evaporator 344 includes a heat exchanger (HE-4) 486, a pressure regulator 452 and a short path evaporator (E-2) 424. The short path evaporator 424 separates the bio-diesel from the glycerol, the unreacted oil and the other impurities. The high purity bio-diesel flows out of the evaporator 424 through the path 426. The evaporator 424 produces unreacted oil contaminated with a trace amount of glycerol through a path 433 for a drum (S-4) 472. The unreacted oil is pumped by means of a gear pump (P-8) 473 through a coolant (HE-6) 475. Depending on the quality of the unreacted oil and / or the amount of impurity in the oil, the unreacted oil can be sent to a waste oil waste drum or sent through a glycerol removal bed (RB-2) 444 to remove the remaining glycerol and recycled to the oil drum D-1. The glycerol removal bed 444 can be, for example, a packed bed filled with a resin that can remove traces of glycerol from the solution. A dual gravity drain grate (DN-1) 457 is placed between the liquid-liquid phase separator (S-2) 456 and the drum 474 to discharge the glycerol automatically. An example of grid 457 is available from Armstrong, Ml, USA. Alternatively, if the drain grid can not be used because the amount of glycerol is very small, a small drum with high level ignition and a low level ignition can be used, both coupled to a solenoid valve at the bottom of the drum for the discharge of glycerol. The crude glycerol in drum 474 can be refined through a vacuum evaporator (not shown in FIG 4) to remove water, unreacted alcohol and inert solvent. The evaporated steam is condensed and absorbed with the condensed liquid drum from evaporator E-1 (and E-2) described above. The residue leaving the crude glycerol evaporator is pure glycerol product suitable for commercial use. Bio-diesel of high purity from the short path evaporator 424 is pumped through a heat exchanger (HE-5) 408, in which cooling water cools the high purity bio-diesel. The final pure bio-diesel product could include at least 99% by weight of alkyl ester. The pure bio-diesel product is stored in a drum of pure bio-diesel product (D-5). During the operation of the processing plant, pure bio-diesel can be recycled through a regeneration path for mixer 210 for reactor 140 when raw blodlesel is not available. The regeneration path is connected to solenoid valve 478 so that pure recycled bio-diesel can be changed when raw bio-diesel is used. 4. Alternative design of a simple stage system FIG. 5 shows an alternative design of a single stage reactor that uses bottom product discharge design. Two liquid drums (S-1) 556 and (S-2) 566, which are switched between vacuum and atmosphere, are used to discharge liquid from a drum 455 coupled to the evaporator. Liquid detectors (not shown) are used on drums 556 and 566 to automatically control the changeover operation to discharge liquids. Double pass solenoid valves 558 and 560 a triple pass solenoid valve 568 regulate the flow of the drum solution 454 to the drums 556 and 566. The valve 560 regulates the flow of liquid from the bottom of the drum 556. In a first period of time, valve 560 is closed and valve 558 is open. The triple pass solenoid valve 568 is configured so that a top opening of the drum 556 is coupled to the vacuum pump (not shown). The solution flows by gravity from the drum 454 to the drum 556. After a predetermined amount of solution is present in the drum 556, the valve 558 is closed. The valve 560 is open and the triple-pass solenoid valve 568 is selected so that ambient air passes a silica gel (or resin) 570 and enters the upper opening of the drum 556. Silica gel or resin 570 removes moisture of the air entering the drum 556. Due to the gravity, the solution in the drum 556 flows inside the drum 566. After the solution flows out of the drum 556 to a predetermined level, the valve 560 is closed, the valve 568 is turned on and valve 558 is reopened. A pump 562 continuously pumps the solution through a binder (CL-1) 454, in which the glycerol drops are agglutinated in large drops and separated from the crude bio-diesel. The pump 562 operates in a similar manner to the gear pump 467 in FIG. 4. The difference is that, for pump 562, the suction pressure is environmental pressure instead of the situation at high centrifugation, as in the case for gear pump 467. This provides more flexibility in the selection of the pump , making it easier to find the appropriate pump. The downflow operation is similar to that given in FIG. 4. A similar design can be used for bottom flows of the short path evaporator (E-2). 5. Two-stage plant Referring to FIG. 6, an example of a two-stage processing plant 1 10B of the configuration shown in FIG. 2B is described in detail below. The final separator 230 in FIG. 2B is omitted in FIG. 6. The first portion of the processing plant 1 10B in FIG. 6 includes a first reactor 140, a first evaporator 324 and a first agglutinator and separator 336B, which operates in a similar manner to the corresponding elements in the F1G. 5. Instead of using a short path evaporator 344 as in FIG. 5, the processing plant 1 10B of FIG. 6 uses a second reactor 140, a second evaporator 324 and a second agglutinator and separator 336B. The second reactor 140, which may be similar to the first reactor 140, includes an enzymatic catalyst, such as a lipase. The first and second reactors 140 may use the same enzymatic catalyst or different enzymatic catalysts. The crude bio-diesel that starts from the glycerol elimination bed RB-2, which removes the glycerol from the crude bio-diesel, travels along a pipe 288 to a second static mixer (SM-2) 210, which is similar to the first static mixer 210 for the first reactor 140. At the same time, a twin outlet pump (P-4) 292 pumps reactive alcohol 130 and inert solvent 120 into the second static mixer (SM-2) 210 at a rate so that the predetermined ratio of reactive alcohol 130 and inert solvent 120 is mix with the crude bio-diesel at the location 290 before entering the static mixer SM-2 210. The output of the static mixer SM-2 210 is sent to the second reactor 140. In the second reactor 140, the reactive alcohol, the oil unreacted and the unreacted oil react to generate more alkyl ester, so that at an outlet of the second reactor 140, less unreacted oil and incomplete oil remains. The output of the second agglutinator and separator 336B includes higher purity bio-diesel, which includes a higher percentage (eg, more than 99% by weight) of alkyl ester. The highest-purity bio-diesel, which could include a trace amount of glycerol, is first cooled in the refrigerant (HE-5) 488 and then passed through the resin bed (RB-3) 489. Resin bed (RB-3) is filled with a resin to eliminate trace amounts of glycerol. The high purity bio-diesel final product 150, which could include, for example, 99 wt.% Alkyl ester, is sent to a drum of high purity product (D-5). The high purity bio-diesel in the D-5 drum can be recycled during operation or supplied to a user. In some examples, the operating conditions for the processing plants 100A (FIGS.4 and 5) and 100B (FIG.6) can be as follows. The first reactor 404 operates at temperatures ranging from 0 ° C to 95 ° C, in which the residence time ranges from 1 to 180 minutes. The first evaporator 451 operates at temperatures lower than 120 ° C and the pressures less than 100 mmHg. The elimination beds 436, 444 and 461 can be operated at temperatures ranging from 20 ° C to 80 ° C, preferably almost at room temperature (for example, 25 ° C). The binders 454 and 456 can be operated at temperatures ranging from 20 ° C to 80 ° C. 6 Operational conditions of Example 6.1 Example 1 The following is an example of operating conditions for a two-stage processing plant described above, in which the raw bio-diesel was recycled for the entry of the first reactor. Thin membrane evaporators were used, and a short path evaporator was not used. Refined soybean oil purchased from a local supermarket was used as regeneration for the processing plant. The amount of water in the refined soybean oil was around 200-300 ppm. Pure methanol anhydride was used as the reactive alcohol. Pure t-amyl alcohol anhydride was used as the inert solvent. The first reactor (R-1) included a packed bed filled with lipase, in which the lipase was TL IM from Novozymes. The residence time of the solution in the first reactor was 50 minutes and the reaction temperature was 25 ° C. The second reactor (R-2) was a packed bed filled with lipase, in which the lipase was Novo 435 from Novozymes. The residence time of the solution in the second reactor was 15 minutes and the reaction temperature was 25 ° C. The evaporators are clean thin membrane evaporators, operating at a temperature of 1 10 ° C and a pressure of 1.0 mmHg abs. , and a rotation speed of 250 revolutions per minute. The final product included 99.10% p of bio-diesel, 0.62% p of monoglycerides, 0.22% p of diglyceride, 0.066% p of triglyceride and the acid number was 0.630 mg KOH / g. 6.2 Example 2 The following is an example of the operating conditions to a simple stage processing plant described above, in which the raw bio-diesel was recycled to the reactor inlet. The alternative evaporator designs were used: (1) a single scintillator drum integrated with a packed bed evaporator and (2) a thin membrane evaporator. The final product was treated by means of a short path evaporator. The regeneration was refined fresh soybean oil with water humidity of 200-300 ppm. The reactor (R-1) was a packed bed filled with lipase. The lipase was TL IM (from Novozymes), the residence time was 53 minutes and the reaction temperature was 25 ° C. When the evaporator (E-1) used a simple flashing drum integrated with a packed bed, the operating temperature was 120 ° C, and the pressure was 5 torr abs. When the evaporator used a thin membrane evaporator without a flashing drum in advance, the operating temperature was 120 ° C, the pressure was 1 torr abs and the rotation rate was 250 revolutions per minute. The final separator used as a short path evaporator (E-2), in which the operating temperature was 120 ° C, the pressure was 0.05 torr abs and the rotation rate was 400 RPM. The final product that was obtained included 99.81% p of bio-diesel, 0.13% p of monoglyceride, 0.06% p of diglyceride and no detectable amount of triglyceride, and the acid number is 0.770 mg KOH / g. 6.3 Example 3 The following is an example of the operating conditions for a single-stage processing plant described above, in which the raw bio-diesel was not recycled. The regeneration was refined fresh soybean oil with water humidity of 200-300 ppm. The reactor (R-1) was a packed bed filled with lpase. The lipase was TL IM (from Novozymes), the residence time was 66.6 minutes and the reaction temperature was 25 ° C. The evaporator (E-1) was a simple flashing drum integrated with packed bed, operating at a temperature of 120 ° C and a pressure of 5 torr abs. The final product that was obtained included 86.55% p of bio-diesel, 6.52% p of monoglyceride, 5.24% of diglyceride and 1.69% p of triglyceride. 6.4 Example 4 The crude bio-diesel product leaving a typical membrane-type binder (pore size in the range of 1 -5 μm) could have an amount of 1, 000-1, 500 ppm glycerol after liquid separation -liquid. The crude bio-diesel can be passed through a bed of resin having a depth of 90 cm, in which the residence time of the fluid in the bed is around 25 minutes. The final concentration of glycerol in the effluent can be less than 15 ppm. The resin that is used can be a type of ion exchange resin, MonoPlus SP1 12, available from Bayer Company, Germany. The saturated bed can be regenerated by means of methanol, ethanol or equivalent materials. 7. Catalyst Cartridges The first and second reactor 140 can use disposable cartridges with enzymatic catalysts, so that the old cartridges can be replaced by new ones when the catalyst becomes ineffective after a long time. The first and second reactor 140 are configured to accept a variety of disposable cartridges, such as those from different vendors or having different types of catalysts. The processing plants 100A to 100D can be designed to have a coupling mechanism that matches the cartridges, so that the cartridges can be easily removed and installed. Different types of enzymatic catalysts can be used, each catalyst associated with a different series of operating conditions, such as flow rate and operating temperature. The bio-diesel fuel production systems could adjust the operating conditions based on the particular type of enzyme catalyst that is being used. Referring to FIG. 7, a bio-diesel fuel production system 702 includes reactors 704, each including a cartridge 706 filled with enzymatic catalyst. The cartridge 706 includes an identifier 708, such as a bar code or a radio frequency identification (RFID) tag that identifies the enzymatic catalyst in the cartridge 706. A reader 710 (eg, a bar code or RFID reader) ) reads the identifier 708, and forwards the identification information to a data processor 712. Based on the identification information, the data processor 712 retrieves the pre-stored operation information from the database 714 and uses the information from operation for controlling a flow control sub-system 716 and a temperature control sub-system 718. The flow control sub-system 716 includes, for example, pumps that determine a flow rate of the oil source and the reactive alcohol flowing through the reactors. In some examples, the identifier 708 could be associated with an enzymatic catalyst that requires a short residence time, so that the data processor 712 controls the flow control sub-system 716 to pump the solutions through the reactors 704 faster. In some examples, the identifier 708 could be associated with an enzymatic catalyst that requires a longer residence time, so that the data processor 712 controls the flow control sub-system to pump the solutions through the reactors 704. more slowly In some examples, the identifier 708 could be associated with an enzymatic catalyst that requires a higher reaction temperature, so that the data processor 712 controls the temperature control sub-system 718 to determine the temperatures of the reactors or the heat exchangers to a higher value. In some examples, the identifier 708 could be associated with an enzymatic catalyst that requires a lower reaction temperature, so that the data processor 712 controls the temperature control subsystem 718 to determine the temperatures of the reactors or exchangers. of lower value. In some examples, the identifier 708 could be associated with pre-stored information that provides an approximate estimate when the cartridge 706 needs to be replaced. The pre-stored information could indicate that the cartridge 706 needs to be replaced after a certain volume of solution has passed the cartridge 706. Based on the flow metrics (not shown) in the system, the data processor 712 determines the volume of solution that has passed to the cartridge 706. When the volume exceeds a certain limit, the data processor 712 displays a message to the user to indicate that the cartridge needs to be replaced. 8 Applications Referring to FIG. 8, an electric power generator 800 includes a processing plant 802 that receives 804 oil source and 805 reactive alcohol and generates 806 bio-diesel. The 806 bio-diesel is sent to a bio-diesel 808 electric power generator, which generates electricity 810 from blo-dlesel 806. A portion of the electricity is sent to the processing plant 802 through a path 812 and used to provide power to various electrical components of the processing plant. The system 802 can be any of the processing plants described above.

An advantage of the 800 electric power generator is that the system can generate electricity with less pollution than those generated by electric power using petroleum-based diesel fuel. If the source of oil includes triglyceride, the generator 800 produces glycerol, water and carbon dioxide as a byproduct. If the oil source includes carboxylic acid, the 800 generator produces only water and carbon dioxide as a byproduct. Referring to FIG. 9, a vehicle 820 includes an 802 processing plant that receives 804 oil source and 805 reactive alcohol, and generates 806 bio-diesel. The 806 bio-diesel is sent to an 814 diesel engine, which converts the bio-diesel into energy kinetic 820 which is sent to a transmission system 816 which transmits the kinetic energy to wheels or propellers to drive the vehicle 820. The vehicle 820 could include an electric power generator (not shown) that converts the kinetic energy of the diesel engine into electricity. The electricity can be used to drive various electrical components of the vehicle 820. The processing plant 802 can be any of the processing plants described above. The vehicle 820 can be, for example, a car, a truck, a train, a ship or an airplane. Referring to the figure FIG. 10, a construction 830, such as a restaurant, includes a food processing unit 834 (such as a kitchen) that receives 832 cooking oil to process food. Recycled oil 836 generated by the food processing unit 834 is sent to an 802 processing plant, which also receives 805 reactive alcohol and produces 806 bio-diesel. An 808 diesel electric power generator receives the bio-diesel and generates electricity, the which is used to drive various electrical components of the food processing unit 834 and the processing plant 802. 9. Alternatives It will be understood that the above description is intended to illustrate and not limit the scope of the invention, which is defined by the scope of the claims. annexes. Other configurations are within the scope of the following claims. For example, double-bore pumps can be replaced by two independent pumps. Static mixers can be replaced by a stirred mixing drum or static mixers of the dosing type. For low-scale production of bio-diesel, a compact static mixer of the dosing type can be used at each mixing point. If the oil source includes a high percentage of water, such as more than 2,000 ppm, the water removal bed can be replaced with a hot air removal apparatus. The water can be removed by removal and the oil cooled before being sent to the reactor. In some examples, when animal fats or oils from high melting point plants are used as regeneration, the fats or oils are first dissolved in the inert solvent. If the oil source includes carboxylic acid, the reaction between the carboxylic acid and the reactive alcohol generates alkyl ester, with water as a by-product. Glycerol is not generated in this circumstance. Because there is no glycerol, the purification of the alkyl ester can be achieved by evaporating the solvent, unreacted alcohol and water. When the oil source includes carboxylic acid, it is not necessary to use separators to separate the bio-diesel from the glycerol or use elimination beds to eliminate the glycerol. In some examples, the bio-diesel can be used as fuel for an internal combustion diesel engine or a gas turbine diesel engine. In some examples, cartridges filled with enzymatic catalysts are used in the reactors of small unit processing plants. For larger commercial units, an in-line charge and descending discharge of lipase is fitted into a system design. In some examples, the evaporator E-1 (FIGS 4-6) can be a simple flashing drum with or without integration of a packed bed design. In other examples, when higher alcohol is used (reactive alcohol or inert solvent), thin membrane evaporators can be used. In some examples, refrigerants (HE-1, HE-3, HE-5 and HE-6) in the same processing plant can be combined into one unit for smaller-scale systems. In some examples, the refrigerants are separated, but placed in parallel in a box and have a common input and a common outlet for the cooling medium, such as cooling water. In some examples, refrigerants are designed as air coolers that use a fan to cool all currents simultaneously. In some examples, a short path evaporator can use a glowing drum at the inlet, similar to that of evaporator E-1. This type of design can reduce the capacitor charge within the short path unit, which means that a higher input rate can be obtained. An external condenser to condense evaporated steam leaving the scintillating drum can be used. The condensate accumulates for the distillate product of the short path unit. The regeneration of the glycerol removal bed can be an on-line processing (such as when parallel designs are used for larger systems) or off-line processing (such as when cartridge-type designs are used for smaller units). During the cessation, the total fuel production system can be flushed with nitrogen to block moisture and air (to reduce the acidification of the bio-diesel or the oil source). In some examples, the glycerol removal resin can be an ion exchange resin, such as Lewatit MonoPlus SP1 12, available from Bayer Chemical, Leverkusen, Germany.

The static mixer can be replaced by a stirred mixer (drum) with its production output regulated by a level control.

Claims (50)

1. CLAIMS 1. An apparatus comprising: a first reactor having an inlet for receiving a mixture comprising a first reagent, a second reagent, a reaction product and an inert solvent that dissolves at least a portion of the first and second reagent, an enzyme to facilitate a reaction between the first and second reagent to generate more reaction product, and an exit to produce the reaction product, including the reaction product received at the inlet and the reaction product generated from the reaction between the first and second reagent; and a return mechanism for sending at least a portion of the reaction product from the outlet back to the entrance.
2. 2. The apparatus of claim 1 wherein the reaction product comprises alkyl ester.
3. 3. The apparatus of claim 2, wherein the return mechanism sends at least a portion of the alkyl ester back to the inlet.
4. 4. The apparatus of claim 2 wherein the mixture includes a solvent that dissolves at least a portion of the first reagent, the second reagent and the reaction product.
5. 5. The apparatus of claim 4 wherein the outlet produces at least the alkyl ester, the solvent and the first unreacted reagent.
6. 6. The apparatus of claim 5, further comprising an evaporator for evaporating the solvent to generate a mixture comprising the alkyl ester and the first unreacted reagent.
7. The apparatus of claim 5 wherein the outlet also produces glycerol outputs.
8. 8. The apparatus of claim 7, further comprising an evaporator for evaporating the solvent to generate a mixture comprising the alkyl ester, the glycerol and the first unreacted reagent.
9. 9. The apparatus of claim 8, further comprising a phase separator for separating the alkyl ester from the glycerol based on the liquid-liquid phase separation. 1.
10. The apparatus of claim 1 wherein the first reagent comprises triglycerides. eleven .
11. The apparatus of claim 1 wherein the first reagent comprises a carboxylic acid.
12. 12. The apparatus of claim 1 wherein the second reagent comprises at least one of the primary and secondary alcohols.
13. The apparatus of claim 1 wherein the first reagent comprises at least one of vegetable oil and animal fat.
14. 14. The apparatus of claim 13 in which the reaction product has a composition that is suitable for use as fuel.
15. 15. The apparatus of claim 1 further comprises a second reactor having an inlet for receiving a mixture comprising second additional reagent and reaction product from the outlet of the first reactor from the outlet of the first, an enzyme to facilitate a reaction between the second reagent and the other components to generate more reaction product, and an output to produce the reaction product, including the reaction product received at the inlet of the second reactor and the reaction product generated from the reaction between the second reagent and the other components.
16. 16. The apparatus of claim 15, further comprising an evaporator for evaporating the inert solvent and at least one of the first unreacted reagent and the second unreacted reagent.
17. 17. The apparatus of claim 16, further comprising a short path evaporator for separating the reaction product from the remaining unreacted reagent.
18. 18. The apparatus of claim 17 wherein the reaction product comprises alkyl ester.
19. 19. The apparatus of claim 18 further comprises a return mechanism for sending at least a portion of the alkyl ester from the outlet of the second reactor back to the entrance of the first reactor.
20. 20. An apparatus comprising: a reactor having an inlet for receiving a mixture comprising reactants, an enzyme for facilitating a reaction between the reagents, and a regeneration mechanism for sending at least a portion of a product from the reaction back to the entrance. twenty-one .
21. The apparatus of claim 20 in which the product of the reaction comprises alkyl ester and the regeneration mechanism sends at least a portion of the alkyl ester back to the inlet.
22. 22. The apparatus of claim 20, wherein the reagents comprise (1) at least one triglyceride and a carboxylic acid, and (2) at least one of, primary and secondary alcohol.
23. 23. The apparatus of claim 20 wherein the enzyme comprises a lipase.
24. 24. A system for generating alkyl ester comprising: a first subsystem including a first reactor having a first inlet for receiving a first mixture comprising a first reagent and an inert solvent for dissolving the first and second reagent, a first enzyme to facilitate the reaction between the first and second reagents to generate a reaction product, and a first outlet to produce the reaction product, the inert solvent and other components; and a second subsystem including a second reactor having a second inlet to receive a second mixture comprising second additional reagent, an inert solvent, at least a portion of the reaction product and the other components of the first outlet, a second enzyme to facilitate a reaction between the second reagent and the other components to generate more reaction product, and a second output to produce the product? of reaction, including the reaction product received at the entrance of the second inlet and the reaction product generated from the reaction between the second reagent and the other components.
25. 25. The system of claim 24 wherein the reaction product comprises alkyl ester.
26. 26. The system of claim 25 also comprises a return mechanism for sending at least a portion of the alkyl ester from the first outlet back to the first entrance.
27. 27. The system of claim 25 also comprises a return mechanism for sending at least a portion of the alkyl ester from the second outlet back to the first entrance.
28. The system of claim 25 wherein the second subsystem comprises a separator for removing at least a portion of components, in addition to alkyl ester, from a first solution outlet from the second inlet to obtain a second solution having at least one 90% by weight of alkyl ester.
29. 29. The system of claim 28 wherein the separator comprises an evaporator.
30. 30. The system of claim 28 in which the separator comprises a liquid-liquid separator.
31. 31 The system of claim 25 wherein the first subsystem comprises a separator for removing at least a portion of components, in addition to the alkyl ester, from a first solution outlet of the first outlet to obtain a second solution having a higher concentration of alkyl ester than the first solution.
32. 32. The system of claim 31, wherein the separator comprises an evaporator.
33. 33. The system of claim 32, wherein the separator comprises a liquid-liquid separator.
34. 34. An apparatus comprising: a reactor having a line of tubing for transmitting a mixture comprising a first reagent, a second reagent, an inert solvent and a reaction product that are in a homogeneous state, a coupler for receiving a cartridge having an inlet for receiving the mixture from the pipeline, an enzyme for facilitating a reaction between the first and second reagent to generate more reaction product, and an outlet for producing the reaction product, including the reaction product received at the inlet and the reaction product generated from the reaction between the first and second reagent; a separation unit for processing the production of the output to produce a solution having a higher percentage of reaction product; and a return mechanism to send at least a portion of the solution back to the pipeline.
35. 35. A system for generating alkyl ester comprising: a first subsystem including a first reactor having a first line of tubing for transmitting a first mixture comprising a first reagent, a second reagent, an inert solvent and alkyl ester which are in a homogeneous state, a first coupler for receiving a first cartridge having a first inlet for receiving the mixture from the pipeline, a first enzyme for facilitating a reaction between the first and second reagent for generating alkyl ester, and a first outlet for producing the alkyl ester, the solvent and other components; and a second subsystem including a second reactor having a second line of pipe to transmit a second mixture comprising second additional reagent, inert solvent and at least a portion of the alkyl ester and the other components of the first outlet, a second coupler to receive a second cartridge having a second inlet to receive the mixture from the second line of pipe, a second enzyme to facilitate a reaction between the second reagent and the other components to generate more alkyl ester, and a second output to produce the alkyl ester.
36. 36. A system for generating alkyl ester comprising: a cartridge for receiving a mixture comprising a first reagent and a second reagent, the cartridge including an enzyme to facilitate a reaction between the first and second reagent to generate a reaction product, cartridge having an identifier; and a regulator for controlling a condition of system operation based on the detector in the cartridge.
37. 37. The system of claim 36 wherein the reaction product comprises alkyl ester.
38. 38. The system of claim 36 wherein the enzyme comprises a lipase.
39. 39. The system of claim 36 wherein the regulator controls a speed of a pump based on the identifier, in which the speed of the pump affects the speed at which the solution passes through the cartridge.
40. 40. The system of claim 36 wherein the regulator controls a heater based on the identifier, in which the heater affects a temperature of the solution.
41. 41 The system of claim 36 wherein the regulator determines when to send a signal indicating that the cartridge needs to be replaced based on the identifier.
42. 42. An apparatus comprising: a cartridge including a lipase, the cartridge configured to be coupled to an alkyl ester generator comprising a mixer for mixing an oil source and a primary alcohol or a secondary alcohol in an organic solvent to form a solution which is passed through the cartridge, in which the oil source includes a triglyceride and the lipas facilitates a reaction between the triglyceride and the primary alcohol or the secondary alcohol to generate an alkyl ester, in which the solution does not pass through the phase separation through the reaction and the glycerol is produced as a by-product, an evaporator for removing the organic solvent and the unreacted primary alcohol or secondary alcohol, a phase separator for separating the alkyl ester from the glycerol, and a second separator for separating the alkyl ester from the unreacted oil source.
43. 43. An apparatus comprising: a cartridge including a lipase, the cartridge configured to be coupled to the alkyl ester generator comprising a mixer for mixing an oil source and a primary alcohol or a secondary alcohol in an organic solvent to form a solution that is passed through the cartridge, in which the oil source includes a carboxylic acid and the lipase facilitates a reaction between the carboxylic acid and the primary alcohol or secondary alcohol to generate an alkyl ester, in which the solution does not pass through the phase separation throughout the reaction and water is produced as a by-product, an evaporator to remove the organic solvent and the unreacted primary alcohol and secondary alcohol, and a separator to separate the alkyl ester from the oil source without reacting
44. 44. The apparatus of claim 43, wherein the separator comprises a short path evaporator.
45. 45. An apparatus comprising: an evaporator having an inlet for receiving a mixture comprising alkyl ester, alcohol, an inert solvent and glycerol, the evaporator for evaporating the inert solvent and the alcohol to generate a solution including an alkyl ester and glycerol, and a separator having an inlet to receive the solution, the separator for separating the alkyl ester from the glycerol based on the liquid-liquid phase separation.
46. 46. An apparatus for producing alkyl ester, comprising: a mixer for mixing a source of oil and a primary alcohol or secondary alcohol in an organic solvent to form a solution, the source of oil including a triglyceride; a reactor for receiving the solution, the reactor including a lipase which facilitates a reaction between the triglyceride or the secondary alcohol to generate an alkyl ester, in which the glycerol is produced as a by-product; an evaporator to remove the organic solvent and the unreacted primary alcohol or secondary alcohol; and a phase separator for separating the alkyl ester from the glycerol.
47. 47. The apparatus of claim 46 also comprises a vehicle, wherein the lipase is immobilized in the vehicle.
48. 48. The apparatus of claim 46 also comprises a return mechanism for allowing at least a portion of the alkyl ester separated by the phase separator to enter the inlet and added to the solution.
49. 49. A method comprising: inserting a cartridge into an alkyl ester generator, the cartridge has an inlet and outlet, and an enzyme placed between the inlet and the outlet; read information encoded in the cartridge; control an operation of the alkyl ester generator based on the information.
50. 50. The method of claim 49 wherein controlling an operation of the alkyl ester generator comprises controlling at least one temperature and flow rate of a solution flowing within the cartridge inlet.