Production of an alkali-glyceroxide-methanol catalyst for biodiesel production
The alkali glyceroxide/methanol catalyst, prepared by mixing alkali metal hydroxide with glycerol under controlled conditions, addresses the high cost and viscosity issues of traditional catalysts, ensuring efficient and cost-effective biodiesel production.
Patent Information
- Authority / Receiving Office
- WO · WO
- Patent Type
- Applications
- Current Assignee / Owner
- REG BIOFUELS GERMANY GMBH
- Filing Date
- 2024-12-05
- Publication Date
- 2026-06-11
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Abstract
Description
[0001] REG-1400US00 / T-12598
[0002] PATENT APPLICATION
[0003] PRODUCTION OF AN ALKALI-GLYCEROXIDE-METHANOL CATALYST FOR BIODIESEL PRODUCTION
[0004] BACKGROUND
[0005] Biodiesel is a renewable, clean-burning petroleum diesel replacement that enhances independence from imported petroleum, reduces greenhouse gas emissions, supports agriculture and rural economies, and creates jobs. While biodiesel provides many benefits, biodiesel production must be economical in order to maintain supply of the advanced biofuel. Producers must adapt to changing market conditions with new processes for converting low-cost feedstocks while meeting stringent product quality specifications.
[0006] One process for making biodiesel involves the transesterification of triglycerides in the oils or fats with a lower alkanol in the presence of a catalyst to produce alkyl ester useful as biodiesel and a glycerin co-product. In this process, the alkyl ester and glycerin are separated, usually by a phase separation, and the lighter phase containing crude biodiesel is refined. Typically refining operations include the removal of residual alkanol, glycerin and other impurities present in the crude biodiesel. A more detailed description of biodiesel production processes are described in US Pat. No. 10,450,533 (Slade et al.) issued on October 22, 2019, the disclosure of which is hereby incorporated by reference.
[0007] While the catalyst for the transesterification may be a basic or acidic catalyst, the use of a basic catalyst is often preferred since the transesterification conditions are generally milder than those required for equivalent conversion rates using acidic catalysts such as sulfuric acid. Typically, alkali metal alkoxide of the lower alkanol is used as the basic catalyst. One existing base catalyst often used in large scale biodiesel production processes is potassium methylate 32% (KM-32). The major disadvantage of using KM-32 is its high cost. Other existing base catalysts used in biodiesel production are alkali glycerolate catalysts. However, alkali glycerolate becomes viscous when it cools and it solidifies under certain temperature and pressure conditions. Viscous catalysts can be difficult and expensive to handle and many biodiesel production facilities are not configured for use with solid catalysts.
[0008] There is therefore a need for a catalyst which is manufactured as a liquid and remains a liquid during biodiesel manufacturing processes and which is cost-effective to manufacture.
[0009] SUMMARY
[0010] One aspect of the invention relates to a process for preparing a base catalyst suitable for catalyzing numerous reactions, including a transesterification reaction for making biodiesel. The process comprises preparing an alkali glyceroxide by contacting an alkali metal hydroxide with an alcohol, such as glycerol. In some embodiments the alkali metal hydroxide and glycerol are mixed at an elevated temperature and under a vacuum. Water is removed from the alkali glyceroxide product producing dried alkali glyceroxide at the desired concentration. The alkali glyceroxide is cooled, but remains heated above ambient temperature to help keep the alkali glyceroxide from solidifying or becoming too viscous. In some embodiments the alkali glyceroxide remains heated above the boiling point of methanol (about 65°C). Methanol is added to the alkali glyceroxide solution before, during, or after the product stream is cooled. Any vaporized methanol condenses and is refluxed back into the solution producing the resultant alkali glyceroxide-glycerol / methanol catalyst solution. The addition of methanol to the alkali glyceroxide helps reduce viscosity and keep the alkali glyceroxide / methanol catalyst product in a liquid state as the catalyst cools to ambient temperatures. In some embodiments the alkali metal is either potassium or sodium.
[0011] Another aspect of the present invention relates to a process for preparing a base catalyst suitable for catalyzing numerous reactions, including transesterification reactions for making biodiesel. The process comprises preparing an alkali (sodium or potassium in some embodiments) glyceroxide by contacting glycerol and alkali hydroxide solution in a reactor with the capacity to operate under vacuum and thereby remove a vapor stream. In some embodiments the molar ratio of alkali hydroxide to alcohol is less than 1 : 1 resulting in a relatively diluted alkali glyceroxide solution. This helps the alkali glyceroxide solution and the alkali glyceroxide / methanol catalyst to remain in its liquid state at cooler temperatures (e.g., 10-25°C). In some embodiments the molar ratio of alkali hydroxide to alcohol is between about 0.2: 1 and 0.6:1. In some embodiments the molar ratio of alkali hydroxide to alcohol is about 0.4:1. The reaction conditions can include heating to temperatures between about 110°C and 150°C and vacuum at pressure between about 130 and 170 mbar. In one embodiment the vacuum pressure is about 150 mbar. The reaction time will depend on reaction temperature and vacuum. The water is removed at an elevated temperature of up to about 130°C. The removal of the water helps drive the reaction forward beyond its equilibrium to produce a solution comprising alkali glyceroxide and excess glycerol. After cooling the alkali glyceroxide solution to between about 80°C -100°C, and preferably to about 90°C, the vacuum is reduced or turned off, and methanol is added to the reactor effluent (or to the reactor, if batch mode), either continuously or in discrete doses. The temperature of the stream / vessel remains above the boiling point of methanol causing some methanol to vaporize. The vapor phase can be actively cooled or passively allowed to cool causing a portion of the vaporized methanol to condense back into the solution. There is no maximum amount of methanol that can be added, other than dictated by practical considerations for the practitioner. The methanol helps reduce viscosity and keep the alkali glyceroxide / methanol catalyst product in a liquid state, even at ambient temperatures (about 20°C), and in some embodiments at or below 10°C. It is believed that some of the methanol reacts with the alkali glyceroxide to form alkali methanolate. Eventually all of the glyceroxide becomes methanolate after enough methanol exposure.
[0012] Another aspect of the present invention relates to a process for preparing a base catalyst suitable for catalyzing numerous reactions, including transesterification reactions for making biodiesel. The process comprises contacting an alkali metal hydroxide with glycerol at an elevated temperature and reduced pressure to produce an alkali glyceroxide reaction mixture comprising alkali metal hydroxide, glycerol, and water. In one embodiment the elevated temperature is between about 110°C and 150°C and the reduced pressure is between about 130 and 170 mbar. Then, distilling water from the alkali glyceroxide reaction mixture to produce alkali glyceroxide, which is cooled to between about 80°C -100°C. Contacting the alkali glyceroxide with an alcohol to produce the alkali glyceroxide alcohol catalyst solution then cooling the alkali glyceroxide alcohol catalyst solution to a desired temperature below 80°C.
[0013] Another aspect of the present invention relates to using the alkali glyceroxide- / alcohol catalyst described above in a transesterification reaction for making biodiesel. The process includes introducing the feedstock to a pre-treatment process to create a pretreated feedstock then reacting the pretreated feedstock in a transesterification reactor with an alcohol and the alkali glyceroxide / methanol catalyst to produce a crude biodiesel. The crude biodiesel may be purified by separation or other suitable means. In some embodiments the separation step may include using at least one of cold filtration, distillation, membrane filtration, and resin filtration. BRIEF DESCRIPTION OF THE DRAWINGS
[0014] FIG. 1 is a process flow diagram showing an exemplary biodiesel production process.
[0015] FIG. 2 is a process flow diagram showing an embodiment for making the alkali glyceroxide / methanol catalyst.
[0016] FIG. 3 is a table showing experimental results of transesterification products produced using a traditional transesterification catalyst compared to transesterification products produced using potassium glyceroxide / methanol catalyst (KGMe-15).
[0017] FIG. 4 is a table showing experimental results of transesterification products produced using potassium glyceroxide / methanol catalyst (KGMe-15) compared to transesterification products produced using sodium glyceroxide / methanol catalyst (NaGMe-10).
[0018] DETAILED DESCRIPTION
[0019] The apparatus, devices, systems, products, processes, and methods of the present invention will now be described in detail by reference to various non-limiting embodiments, including the figures which are exemplary only. For the purposes of promoting an understanding of the principles of the disclosure, reference will now be made to embodiments and specific language will be used to describe the same. It will nevertheless be understood that no limitation of the scope of the disclosure is thereby intended, such alteration and further modifications of the disclosure as illustrated herein, being contemplated as would normally occur to one skilled in the art to which the disclosure relates. As used in the specification, articles “a” and “an” refer to one or to more than one (i.e., at least one) of the grammatical object of the article. By way of example, “an element” means at least one element and can include more than one element.
[0020] Unless otherwise indicated, all numbers expressing dimensions, capacities, and so forth used in the specification and claims are to be understood as being modified in all instances by the term “about.” “About” is used to provide flexibility to a numerical range endpoint by providing that a given value can be “slightly above” or “slightly below” the endpoint without affecting the desired result. The term “about” in association with a numerical value means that the numerical value can vary by plus or minus 5% or less of the numerical value.
[0021] Throughout this specification, unless the context requires otherwise, the word “comprise” and “include” and variations thereof (e.g., “comprises,” “comprising,” “includes,” “including”) will be understood to imply the inclusion of a stated component, feature, element, or step or group of components, features, elements, or steps but not the exclusion of any other integer or step or group of integers or steps.
[0022] As used herein, “and / or” refers to and encompasses any and all possible combinations of one or more of the associated listed items, as well as the lack of combinations were interpreted in the alternative (“or”).
[0023] Recitation of ranges of values herein are merely intended to serve as a succinct process of referring individually to each separate value falling within the range, unless otherwise indicated herein. Furthermore, each separate value is incorporated into the specification as if it were individually recited herein. For example, if a range is stated as 1 to 50, it is intended that values such as 2 to 4, 10 to 30, or 1 to 3, etc., are expressly enumerated in this disclosure. These are only examples of what is specifically intended, and all possible combinations of numerical values between and including the lowest value and the highest value enumerated are to be considered to be expressly stated in this disclosure.
[0024] The present invention may be practiced by implementing process steps in different orders than as specifically set forth herein. All references to a “step” may include multiple steps (or sub steps) within the meaning of a step. Likewise, all references to “steps” in plural form may also be construed as a single process step or various combinations of steps.
[0025] The present invention may be practiced by implementing process units (e.g., a distillation apparatus or reactor vessel) in different orders than as specifically set forth herein. All references to a “unit” may include multiple units (or subunits) within the meaning of a unit. Likewise, all references to “units” in plural form may also be construed as a single process unit or various combinations of units. As used herein, the particular product and the unit / stream holding / transferring the product sometimes have the same reference number.
[0026] FIG. 1 shows an exemplary process for making an alkali glyceroxide / methanol catalyst 60 suitable for catalyzing numerous reactions, including transesterification reactions for making biodiesel. The process comprises preparing an anhydrous alkali glyceroxide by contacting an alcohol 10, such as glycerol, with an alkali metal hydroxide 20 to produce alkali glyceroxide and water, wherein glyceroxide refers to the anionic species resultant from deprotonation of the alcohol 10. The alkali metal hydroxide 20 may a dry material or it may be an aqueous solution prior to being introduced to the alcohol 10. In this illustrative example, the alkali metal is potassium and the glyceroxide produced is potassium glyceroxide (CsH^OFfLOK), however, other suitable alkali metals can be used, including sodium wherein the glyceroxide produced is sodium glyceroxide (CML(OH)2ONa). The alcohol 10 may be any suitable polyol or alcohol. In one embodiment the alcohol is any suitable polyol or alcohol having a boiling point higher than the boiling point of water
[0027] (higher than 100°C) so water can be distilled (boiled) off without losing any of the alcohol 10. Removing water from the alkali glyceroxide solution helps drive the reaction forward beyond its equilibrium (which favors the formation of the hydroxide).
[0028] In embodiments using glycerol as the alcohol 10, any suitable source and purity of glycerol can be used. The glycerol may be may be reagent grade glycerol or it may be sourced from a used cooking oil or other food waste oil. In some embodiments the glycerol is derived from a biodiesel production process (where glycerol is the co-product with biodiesel). In addition to convenience, using glycerol from a biodiesel production process helps reduce risk of contamination which could occur if a different polyol / heavy alcohol was used. In other words, glycerol is already at the production facility and the glycerol from the catalyst can be directed to join the new glycerol in its part of the biodiesel production process.
[0029] In some embodiments the molar ratio of alkali hydroxide 20 to alcohol 10 is less than 1 : 1 resulting in a relatively diluted alkali glyceroxide solution. This helps the alkali glyceroxide solution and the alkali glyceroxide / methanol catalyst 60 to remain in its liquid state at cooler temperatures (e.g., 10-25°C). In some embodiments the molar ratio of alkali hydroxide 20 to alcohol 10 is between about 0.2: 1 and 0.6: 1. In some embodiments the molar ratio of alkali hydroxide 20 to alcohol 10 is about 0.4:1.
[0030] In the embodiment shown in FIG. 1, alcohol 10 and potassium hydroxide 20 are combined in a reactor 40 at an elevated temperature (relative to ambient temperature) and under a vacuum (reduced pressure relative to ambient pressure). The preparation of the alkali glyceroxide solution may be continuous, semi-continuous, or batch. The reactor 40 may be a batch reactor such as a distillation reactor wherein the solution remains in the reactor 40 for a predetermined amount of time (as described below). In other embodiment the reactor 40 may be a continuous flow reactor such as a jacketed continuous stirred-tank reactor.
[0031] In one embodiment the solution is heated to a temperature that is about between 110°C and 150°C. In another embodiment the temperature is about between 125°C and 135°C. In another embodiment the temperature is about 130°C. In one embodiment the reduced pressure vacuum may be between about 130 and 170 mbar. In another embodiment the reduced pressure vacuum in the reactor 40 is about between 145-155 mbar. In another embodiment the reduced pressure vacuum is about 150 mbar. The elevated temperature and reduced pressure cause water / steam to be distilled out of the reactor 40 in stream 46 which is directed to water condenser 48 and water recovery. As noted above, removing water from the alkali glyceroxide solution helps drive the reaction forward beyond its equilibrium (which favors the formation of the hydroxide). Further, lower water content in the final catalyst product makes the catalyst more efficient. A lower water content in the catalyst means less catalyst is used up in the transesterification reaction. In some embodiments the alkali glyceroxide solution has a water content of less than 1.0%. In other embodiments the alkali glyceroxide solution has a water content of less than 0.5%. The elevated temperature and reduced pressure also help the anhydrous alkali glyceroxide (being formed in the reactor 40) remain in a liquid state with low enough viscosity that it can flow out of the reactor 40 to downstream parts of the process / system.
[0032] The reaction mixture inside the reactor 40 comprises the reactants (potassium hydroxide and glycerol), the products (anhydrous alkali glyceroxide and water). The longer the reactants are in contact with each other, the more alkali glyceroxide product is produced. In embodiments using batch distillation reactors, distillation continues removing water from the reaction mixture until the reaction mixture comprises the desired concentration of alkali glyceroxide product. In other words, the composition of the reaction mixture changes over the residence time of the reactants inside the reactor 40 and over the duration of the distillation. The mixture remains in the reactor 40 for a predetermined amount of time until the reaction mixture has mostly converted to alkali glyceroxide. In some embodiments the reaction mixture remains in the reactor for about between about 2-4 hours, and in one embodiment about 3 hours. In some embodiments the solution is about between 15-25% alkali glyceroxide solution. In some embodiments the solution is about 20% alkali glyceroxide solution.
[0033] The reaction mixture may be heated by any suitable means. In the embodiment shown in FIG. 1 , pump 42 directs the reaction mixture stream through line 45 from the reactor 40, which passes through a heat exchanger 44 to heat the stream. The heated reaction mixture stream is then reintroduced to the reactor 40 and a condensate stream is directed to waste or water collection. In this manner, the reaction mixture in the reactor 40 recirculates through the heating loop to heat the contents of the reactor 40.
[0034] The alkali glyceroxide solution is cooled after reaching its desired concentration and water content. In some embodiments the potassium glyceroxide solution remains in the reactor 40 for a predetermined amount of time until the temperature of the solution cools to about 85- 95°C, and in some embodiments to about 90°C. In some embodiments a heat exchanger or other suitable means may be used to cool the reaction mixture in the reactor 40. The reaction mixture is cooled to a temperature that is lower than the temperature at which the potassium glyceroxide solution was produced, but still higher than the boiling point of methanol (about 65°C) (since methanol is subsequently introduced to the reactor effluent stream) and high enough to keep the anhydrous alkali glyceroxide in a liquid state with low enough viscosity that it can flow out of the reactor 40 to downstream parts of the process / system. In one embodiment, cooling the glyceroxide solution comprises adding methanol to the glyceroxide solution wherein the methanol is above its boiling point (about 65 °C) but below the reaction temperature of the glyceroxide solution. This cools the solution and increases the pressure without allowing air into the system. In another embodiment the vacuum pressure is reduced by introduction of inert gas (e.g., nitrogen, argon). This could be done in batch mode in the same reactor 40 used to react the alcohol 10 with the alkoxide. Or it could be done in separate continuous stirred-tank reactors.
[0035] The reduced pressure vacuum is turned off and the product pump 52 directs the cooled alkali glyceroxide effluent toward one or more mixers 54, which may be static mixers, where the liquid potassium glyceroxide effluent is mixed with methanol 30. In some embodiments about 20-40% methanol is mixed with the potassium glyceroxide effluent stream passed by line 50. In some embodiments about 33% methanol is mixed with the potassium glyceroxide effluent stream. Some of the methanol 30 vaporizes since the temperature of the potassium glyceroxide effluent stream remains above the boiling point of methanol 30.
[0036] The stream is cooled using a heat exchanger 56 or any other suitable means. The vaporized methanol 30 condenses back into the solution under reflux producing the liquid alkali glyceroxide-glycerol / methanol catalyst solution 60. In some embodiments the methanol 30 dilutes the glyceroxide / methanol catalyst solution 60 to about between 10-25% alkali glyceroxide / methanol catalyst solution 60. In some embodiments the alkali glyceroxide- glycerol / methanol catalyst 60 stream is recycled upstream through line 58 to pass through the one or more mixers 54 and the heat exchanger 56 again for further mixing and cooling. The addition of methanol 30 to the alkali glyceroxide solution helps reduce viscosity and keep the alkali glyceroxide / methanol catalyst 60 product in a liquid state. There is no maximum amount of methanol that can be added, other than dictated by practical considerations. The methanol helps reduce viscosity and keep the alkali glyceroxide / methanol catalyst product in a liquid state, even at ambient temperatures (about 18- 25°C), and in some embodiments between about 10-25°C. In some embodiments the alkali glyceroxide / methanol catalyst remains in a liquid state at or below 10°C.
[0037] An exemplary method 100 with reference to FIG. 2 is outlined for processing crude feedstock 105 into glycerin 145 and purified biodiesel 160 meeting commercial product specifications. Crude feedstocks 105 containing various impurities sometimes require pretreatment and / or FFA refining before being subjected to a transesterification process to convert the refined feedstock to crude biodiesel 150 and finally a biodiesel purification process to make high quality purified biodiesel 160 that meets multiple commercial specifications. The crude feedstock 105 arrives at the biodiesel production facility and is discharged into crude feedstock storage. Compatible feedstocks may be combined and stored in a shared tank before being processed. Crude feedstock 105 first undergoes a feedstock pretreatment process 110 that depends on its FFA content and other properties to produce a pretreated feedstock 115.
[0038] The pretreated feedstock 115 may then be subjected to an FFA refining process 120 which removes and / or converts FFA by way of: FFA stripping (dashed line 2) or esterification / glycerolysis (dashed line 3) to yield a refined feedstock 125. Optionally, FFA refining 120 may yield a stream of crude biodiesel 150 in the case of FFA stripping followed by esterification of the fatty acid distillate. As another option, FFA refining 120 may yield a stream of glycerides or refined feedstock 125 in the case of FFA stripping followed by glycerolysis of the fatty acid distillate. In one embodiment, as shown by dashed line 1 , pretreated feedstock 115 having sufficiently low levels of FFA to be categorized as refined feedstock (i.e., the crude feedstock was chemically refined to remove FFA in feedstock pretreatment 110 or was refined elsewhere) bypasses the FFA refining unit 120. Refined feedstock 125 is processed in a transesterification process 130 with a catalytically effective amount of a base catalyst to yield crude biodiesel 150 and crude glycerin 135. The catalyst may be the alkali glyceroxide / methanol catalyst described in this disclosure. Crude glycerin 135 is refined in a glycerin refining unit 140 yielding glycerin 145 which may be recycled into the FFA refining process 120 for glycerolysis. Crude biodiesel 150 undergoes a final biodiesel refining process 155 to produce a commercially - acceptable purified biodiesel product 160. Wet alcohol from biodiesel refining 155 and glycerin refining 140 is sent to an alcohol recovery unit 165 to separate water 175 and recover dry alcohol 170.
[0039] EXAMPLES
[0040] FIG. 3 shows a first experiment wherein products obtained in a dual reactor transesterification process using traditional catalyst potassium methlate 32% (KM-32) are compared to and the products obtained in the same transesterification process using the 15% potassium glyceroxide / methanol catalyst described in this disclosure (KGMe-15). The analysis of the two tests shows similar results. The conversion rate of KM-32 is only slightly better than KGMe-15 at the same stoichiometric dosage. However, this difference is not significant.
[0041] FIG. 4 shows a second experiment wherein products obtained in a dual reactor transesterification process using a 10% sodium glyceroxide / methanol catalyst (NaGMe-10) are compared to products obtained in the same transesterification process using potassium glyceroxide / methanol catalyst (KGMe-15). In this experiment, the glyceroxide catalyst based on sodium was also produced in the laboratory. However, the sodium concentration was reduced due to salt precipitation and high viscosity of the catalyst. When preparing the sodium hydroxide (50%) and glycerol mixture, a 15% sodium glyceroxide solution was produced. This was then further diluted with methanol to 10% after evaporation of the water to produce an NGMe-10 catalyst. FIG. 4 shows the results of the second experiment wherein transesterification with the two catalysis shows similar results. The NaGMe-10 produced slightly more triglycerides than the KGMe-15. However, the difference is not significant and the experimental results show both
[0042] NaGMe-10 and KGMe-15 to be highly effective transesterification catalysis.
[0043] Having thus described the invention in connection with the preferred embodiments thereof, it will be evident to those skilled in the art that various revisions can be made to the preferred embodiments described herein without departing from the spirit and scope of the invention. It is my intention, however, that all such revisions and modifications that are evident to those skilled in the art will be included with in the scope of the following claims.
Claims
CLAIMSWhat is claimed is as follows:
1. A process for preparing an alkali glyceroxide methanol catalyst solution, said process comprising: contacting an alkali metal hydroxide with glycerol in a reaction mixture to produce alkali glyceroxide; contacting the alkali glyceroxide with methanol to produce the alkali glyceroxide methanol catalyst solution.
2. The process of claim 1 wherein the alkali metal is either potassium or sodium.
3. The process of claim 1 wherein the mixture comprises the alkali metal hydroxide, glycerol, water, and alkali glyceroxide.
4. The process of claim 3 wherein the step of preparing the alkali glyceroxide further includes distilling water from the reaction mixture.
5. The process of claim 3 wherein the step of preparing the alkali glyceroxide further includes heating the reaction mixture6. The process of claim 5 wherein the reaction mixture is heated to between about 110°C and 150°C.
7. The process of claim 3 wherein the step of preparing the alkali glyceroxide is performed under a vacuum.
8. The process of claim 7 wherein the vacuum is between about 130 and 170 mbar.
9. The process of claim 1 wherein the alkali glyceroxide methanol catalyst is liquid at 10°C.
10. The process of claim 1 wherein the alkali glyceroxide is produced in a distillation chamber.
11. The process of claim 10 wherein the step of preparing the alkali glyceroxide further includes distilling water from the distillation chamber.
12. The process of claim 1 wherein the alkali glyceroxide methanol catalyst is between about 10-20% alkali glyceroxide dissolved in methanol.
13. The alkali glyceroxide-glycerol / methanol catalyst produced by the process of claim 1.
14. A process for preparing an alkali glyceroxide methanol catalyst solution, said process comprising: contacting an alkali metal hydroxide with glycerol in a reaction mixture to produce alkali glyceroxide, wherein the reaction mixture comprises alkali metal hydroxide, glycerol, water, and alkali glyceroxide; distilling water from the reaction mixture to increase the concentration of alkali glyceroxide in the reaction mixture while heating the reaction mixture and subjecting the reaction mixture to a vacuum; cooling the reaction mixture; contacting the alkali glyceroxide in the reaction mixture with methanol to produce the alkali glyceroxide methanol catalyst solution; cooling the alkali glyceroxide methanol catalyst solution.
15. The process of claim 14 wherein the alkali metal is either potassium or sodium.
16. The process of claim 14 wherein the reaction mixture is heated to between about 110°C and 150°C.
17. The process of claim 14 wherein the vacuum pressure is between about 130 and 170 mbar.
18. The process of claim 14 wherein the alkali glyceroxide methanol catalyst is liquid at 20°C.
19. The process of claim 14 wherein the reaction mixture is cooled to between about 80°C - 100°C.
20. The process of claim 14 wherein the alkali glyceroxide methanol catalyst solution is cooled to below 80°C21. The process of claim 14 wherein the alkali glyceroxide is produced in a distillation chamber.
22. The process of claim 1 wherein the alkali glyceroxide methanol catalyst is between about 10-20% alkali glyceroxide dissolved in methanol.
23. The alkali glyceroxide-glycerol / methanol catalyst produced by the process of claim 1.
24. The process of claim 14 further comprising using an effective amount of the alkali glyceroxide-glycerol / methanol catalyst in a transesterification step of a biodiesel production process.
25. A process for producing biodiesel using an alkali glyceroxide methanol catalyst solution, said process comprising: introducing a feedstock to a pre-treatment process to create a pretreated feedstock; reacting the pretreated feedstock in a transesterification reactor with an alcohol and the alkali glyceroxide / methanol catalyst to produce a crude biodiesel; purifying the crude biodiesel to produce a purified biodiesel.