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WO2024205513A1 - Procédé et application de séparation d'ester méthylique et de glycérine utilisés dans un procédé de purification de biodiesel - Google Patents

Procédé et application de séparation d'ester méthylique et de glycérine utilisés dans un procédé de purification de biodiesel Download PDF

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Publication number
WO2024205513A1
WO2024205513A1 PCT/TH2023/050006 TH2023050006W WO2024205513A1 WO 2024205513 A1 WO2024205513 A1 WO 2024205513A1 TH 2023050006 W TH2023050006 W TH 2023050006W WO 2024205513 A1 WO2024205513 A1 WO 2024205513A1
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WO
WIPO (PCT)
Prior art keywords
raw
glycerin
tank
reactor
mixing
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/TH2023/050006
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English (en)
Inventor
Narongsak Tonmukayakul
Wuttiphan BENJATHANYAPOL
Rujipas BOONAREE
Voravee THUMCHAI
Pudit BURANAPIN
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Esg Jet Thailand Co Ltd
Original Assignee
Esg Jet Thailand Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Esg Jet Thailand Co Ltd filed Critical Esg Jet Thailand Co Ltd
Priority to PCT/TH2023/050006 priority Critical patent/WO2024205513A1/fr
Publication of WO2024205513A1 publication Critical patent/WO2024205513A1/fr
Anticipated expiration legal-status Critical
Pending legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
    • C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
    • C11C3/003—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fatty acids with alcohols
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/003—Marking, e.g. coloration by addition of pigments
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Definitions

  • the purpose of this invention is to solve the problem of biodiesel production in Thailand, while meeting the requirement for high-quality biodiesel with no need of distillation for purity, as follows:
  • This invention integrates technical knowledge with experience in the biodiesel production industry in Thailand to devise a reactor that can produce biodiesel with a purity level higher than 98.0% and a monoglyceride level of less than 0.3%.
  • the biodiesel can be stored in a large tank with no sterol glucosides sedimentation.
  • the Invention background is indicated as follows:
  • the distributers of commercialbiodiesel production technology currently situated in Thailand design a form of a water-based biodiesel-rinsing system, receiving biodiesel quality certification in accordance with international standards.
  • the monoglycerides in particular, do not exceed 0.7%.
  • some distributers of commercial-biodiesel production technology who rinse with water and boil out the moisture from the biodiesel are not able to solve the problem of the sterol glucosides generated by agglomeration, which cause the biodiesel in the product storage tank to become cloudy. Accordingly, the problem was solved by designing a biodiesel purification process by distillation to a biodiesel purity level using high heat under a distillery pressure below atmospheric. This process requires the use of much higher heat energy in the production process and, therefore, a higher production cost, as well.
  • Figure 1 shows vertical cross-section of all components making up a continually operating transesterification reactor capable of producing biodiesel with purity higher than 98.0% with a monoglyceride level less than 0.3%; the biodiesel thus produced is stored in a large tank with no agglomeration of sterol glucosides sediments. It is composed of the following five main sets of machinery and equipment:
  • Figure 2 shows design illustration of the mixing head for the mixture of raw glycerin and raw methyl esters in the second-cycle separation tank.
  • the biodiesel thus produced can be stored in a large tank with no sterol glucosides sedimentation.
  • the relationship among each of the 30 components performing the various functions can be explained according to the numbers shown in Figure 1 of the invention process diagram as follows:
  • the reactor structure was designed in accordance with the ASME Section 8 pressurized tank standard with a diameter calculated to be compatible with laminar, non-turbulent, flow rates. For example, for a flow rate of 600,000 kilograms per day through the reactor, a cylindrical reactor with a diameter no less than 100 centimeters should be used. Use of a larger size would be an unnecessary waste of material.
  • the interior of this reactor consists of four integrated sets assembled together as the “first-cycle transesterification reactor 1,” with each set consisting of five components, namely, the “reactor-entrance mixing pipe and the reactor-interior mixing pipe 2,” “the first of three mixing plates 3,” “the second of three mixing plates 4,” “the third of three mixing plates 5” and “mixing-chamber separator plate 6.”
  • These components have the function of helping the transesterification to proceed until the amount of the raw biodiesel methyl esters issuing from the “first-cycle transesterification reactor 1” has a minimal purity level of 96.5%, with a monoglyceride level of less than 0.7%.
  • This component consists of a steel pipe with a diameter allowing the passage of the mixture through the pipe, but without allowing a pipe flow rate higher than the critical value as established by chemical-industry piping-design standards. For example, for a flow rate through the reactor of 600,000 kilograms per day, a steel pipe with a diameter of at least 10 centimeters should be used.
  • the rapid mixing pipe can be simply designed in many shapes and forms such as T-shape connection and/or other design that will allow rapid mixing profile to occur within the pipe reactor itself.
  • a fixed mixing blade will be inserted to alternately reverse the direction of flow within the pipe in order to help generate a continual mixing action.
  • the mixing pipe consists of four sections, which are joined together, namely:
  • the first pipe is the outlet pipe, designed for an upward flow.
  • the lower end is joined to the reactor for the “first combination set” for the first combination set. It is also joined to the “mixing-chamber separator plate 6” of the “second combination set,” the “third combination set” and the “fourth combination set.”
  • the upper end of the first pipe is welded to the “second pipe.”
  • the second pipe has the function of dividing the flow coming from the first pipe. It will be installed in a horizontal position and welded to the end of the first pipe, forming a symmetrical T-shape (1) so that it can be able to divide the outflow on both sides.
  • This tubing section will be of the same size as the first pipe.
  • the third pipe serves as a secondary distribution pipe in which its center is connected to the end of the second pipe in a T-shape (I).
  • the third pipe is placed in a horizontal position.
  • the size of the third pipe it has one half the diameter of the “second pipe.”
  • the fourth pipe, the final mixing pipe will be welded to the end of the third pipe, thus totaling four tubing sections. It will be installed vertically with its outer end turned downward. The ends of all four tubing sections will be welded with approximately * pipe reducers to accelerate the flow velocity of the mixture at the end of the exit pipe.
  • the end of the pipe will be set at a distance from partition number 3 of approximately twice the diameter of the pipe in order to generate turbulent mixing by swirling back upon impact with the reactor for the “first combination set,” and will be welded to the “mixing-chamber separator plate 6” of the “second combination set,” the “third combination set” and the “fourth combination set.”
  • This plate uses a steel plate with a thickness of 6 millimeters, formed into a round shape with a diameter that will permit it to be welded and fitted to the internal diameter of the reactor.
  • This mixing plate is designed with an angle from 2° to 8° for promoting a rapid drainage of the methyl ester and glycerin during the separation phase. It will be set at a distance equal to * of the diameter of the reactor from the weld of the semicircular steel plate closing off the reactor for the “first combination set.” It will be set apart from “mixing-chamber separator plate 6” of the “second combination set,” the “third combination set” and the “fourth combination set”.
  • Three holes will be drilled in the center of this mixing plate with a diameter equal to % of the diameter of the reactor in order to help in the moderately rapid mixing with the raw glycerin flowing out from the second mixing plate (4) at the top.
  • a drainage pipe is placed at the end of the mixing plate at the distance from the chamber wall of 3 inch spacing and with the ID of 1 inch from promoting a better drainage of methyl ester and glycerin..
  • This plate uses a steel plate with a thickness of 4 millimeters, formed into a round shape with a diameter that will permit it to be welded and fitted to the internal diameter of the reactor. It will be set at a distance equal to ’A of the diameter of the reactor from the “first of the three mixing plates 3.” Three holes with a diameter equal to % of the diameter of the reactor tank is drilled into the center and on the space between the central hole to wall of the mixing chamber in order to slow the upward flow rate of the mixture and promote a laminar flow regime, instead.
  • the downward-rolling laminar flow velocity will reduce in speed extensively, causing the raw glycerin resulting from the reaction to begin to separate out from the raw methyl ester mass as tiny raw-glycerin pellets.
  • the glycerin is still suspended in the raw methyl ester mass and is capable of flowing upward through the third mixing chamber separator plate on the top side (5).
  • This mixing plate is designed with an angle from 2° to 8° for promoting a rapid drainage of the methyl ester and glycerin during the separation phase.
  • a drainage pipe is placed at the end of the mixing plate at the distance from the chamber wall of 3 inch spacing and with the ID of 1 inch from promoting a better drainage of methyl ester and glycerin.
  • This plate uses a steel plate with a thickness of 4 millimeters, formed into a round shape with a diameter that will permit it to be welded and fitted to the internal diameter of the reactor. It will be set at a distance equal to * of the diameter of the reactor from the “second of the three mixing plates 4.” A hole will be drilled in the center of this mixing plate with a diameter equal to * of the diameter of the reactor in order to help in retarding the upward flow of the mixture and to help the raw glycerin that has formed to begin to separate out from the raw methyl esters and can also enable the passage of the raw glycerin flowing out from mixing-chamber separator plate above it down to that “second of the three mixing plates 4”. A drainage pipe is placed at the end of the mixing plate at the distance from the chamber wall of 3 inch spacing and with the ID of 1 inch from promoting a better drainage of methyl ester and glycerin.
  • This partition uses a steel plate with the same thickness of the “first-cycle transesterification reactor 1.” It is cut into a round sheet with a diameter that will permit it to be welded and fitted to the internal diameter of the reactor. It will be set at a distance equal to * of the diameter of the reactor from the “third of the three mixing plates 5” of the mixing chamber below it. Also, the mixing-chamber separator plate must be very firmly welded to reactor with good strength by notching the rim of this mixing chamber at a 45-degree angle to form an upward-facing braided groove.
  • This mixing -chamber separator plate can then be welded all around the reactor at the full thickness of the mixing-chamber separator plate to ensure its mechanical strength, since this mixing -chamber separator plate must withstand the force of the flow impacting upon it from bottom to top from the that second glycerin extraction chamber.
  • a hole will be drilled in the center of this mixing plate with a diameter equal to the outer diameter of the “reactor internal mixing pipe 2” and the “first pipe” by welding together the mixingchamber separator plate and the mixing pipe along the entire outer circumference of the pipe both above and below those same mixing -chamber separator plates.
  • First-cycle high-speed mixer 7 This device has the function of combining pure distilled fat into a mixture of preprepared methanol and sodium methylate so that all ingredients will be quickly mixed into a homogenous mass. The ingredients which are now a single homogeneous mass will then flow out from the mixer into the “first-cycle transesterification reactor 1” through the “mixture delivery pipe from the high-speed mixer 14.”
  • the controller consists of important devices automatically functioning together which are mass flow-rate meter, a control valve and a flow rate controller.
  • the mass flow-rate meter is positioned at the front of the control valve at all times with a constant controlled flow rate. This rate is used as benchmark for making adjustments to the flow rates of the methanol and sodium methylate.
  • Purified Methanol requires no more than 500 milligrams by weight of moisture or other substances per 1.0 kilogram of methanol and involves the use of certain important devices operating together automatically which are a mass flow-rate meter, a control valve and a flow rate controller.
  • the mass flow-rate meter is positioned at the front of the control valve at all times with a constant controlled flow rate equal to 1.5% of the flow rate of the purified palm oil.
  • this controller requires a concentration of 30% sodium methylate in methanol combined with certain important devices operating together automatically which are a mass flow-rate meter, a control valve and a flow rate controller. It must be positioned so that the mass flow-rate meter is situated on the front side of the Valois control at all times with a constant controlled flow rate equal to 1.5% of the flow rate of the purified palm oil.
  • This mixer has a function of combining the raw biodiesel methyl esters from the “raw glycerin separation tank 17” into a pre-prepared mixture of methanol and sodium methylate such that all ingredients quickly dissolve into a single homogeneous mass. This single homogeneous mixture will then flow out from the mixer into the second reactor.
  • “Purified methanol feed controller 12” The moisture content of the purified methanol must not exceed 500 milligrams by weight per 1.0 kilogram of methanol and involves the use of certain important devices operating together automatically which are a mass flow-rate meter, a control valve and a flow rate controller.
  • the mass flow-rate meter is situated on the front side of the control valve at all times with a constant controlled flow rate equal to 5.0% of the inflow rate of the purified palm oil.
  • this controller requires a concentration of 30% sodium methylate in methanol combined with certain important devices operating together automatically which are a mass flow-rate meter, a control valve and a flow rate controller.
  • the mass flow-rate meter is situated on the front side of the control valve at all times with a constant controlled flow rate equal to 0.5% of the flow rate of the purified palm oil.
  • the length of pipes between the high-speed mixer and the reactor-entrance must be the shortest.
  • the mixer shall be installed in the fixed-blade mixing pipe in order to prevent separation of the mixture, which would unnecessarily reduce the efficiency of the transesterification reaction.
  • the pipe network consists of a pipe connecting the first-cycle reactor outlet to the “raw glycerin separation and disposal tank 17.”
  • the pipe connecting the front side of the outflow flange from the “first-cycle transesterification reactor 1” and the pipe reducer prior to connection to the automatic control valve are of the same size.
  • the size of the control valve will be calculated to be compatible with the flow rate of the mixture being discharged from the “first- cycle transesterification reactor 1”.
  • the discharge pipe of the control valve will be expanded to a two-fold size of the inlet pipe of the reactor 1 in order to help retard the movement of the mixture in the pipe before entering to the “continual raw glycerin extraction and disposal 17”.
  • This control valve has the function of maintaining a constant internal pressure in the “first- cycle transesterification reactor 1” and a pressure higher than the methanol gas pressure at a temperature of 100 °C in order to prevent the methanol from changing its state from liquid to gas. This prevents the transesterification reaction from taking place, since the amount of liquid methanol for the reaction to take place would then be reduced.
  • This component has the function of transporting the raw methyl ester into the “second- cycle high-speed mixer 11” for the purpose of blending with the methanol and sodium methylate prior to feeding it into the second reactor set through pipe number 14.
  • This component is designated as a high-pressure tank and may have either a horizontal or an upright shape on the machine installation site.
  • the tank has a horizontal form, it has been determined that the mixture flowing out from the “first-cycle transesterification reactor 1” should flow into this tank in the middle of the tank on one of its sides. In this way, the mixture will extract the raw glycerin from the natural raw methyl esters under the force of gravity.
  • the raw glycerin has a high polarity and a greater density than the raw methyl esters, which have a much lower polarity and is thus able to separate out through gravitational force. The raw glycerin will thus separate and accumulate on the bottom of the separation tank.
  • the separation tank requires designing the separation tank to have a minimum passage flow time of 30 minutes, but, because the tank is shaped horizontally, there are not much of a bond between the raw glycerin and raw methyl esters in order to prevent the contamination from the low-purified biodiesel methyl esters with a presence of monoglyceride substances in excess of 0.3% mixed into the raw glycerin.
  • the design of the horizontal separation tank must include a tank navel pipe which is a pipe with a size approximately equal to the size of the “first-cycle transesterification reactor 1” The height of the pipe leading down from the separation tank on the opposite side of the inlet pipe will be at least i of the height of the “first-cycle transesterification reactor 1”.
  • the raw biodiesel will flow out from the top side of the tank on its other side, which is situated opposite to the inlet pipe.
  • This indicator functions by transmitting a bond-level signal to the bond-level controller so that it will remain constant, by continually discharging the raw glycerin out from the “continual raw glycerin separation and disposal tank 17.”
  • “Raw glycerin discharge control pipe and valve 19” This component has the function of automatically controlling the disposal of raw glycerin from the “continual raw glycerin separation and disposal tank 17.” It works in conjunction with “level indicator 18” with the important objective of maintaining the bond within the raw glycerin on the underside of the separation tank in order to keep the raw biodiesel methyl esters from flowing out along with the raw glycerin.
  • This component has the function of maintaining a constant pressure within the interconnected piping system, which includes the first-cycle reactor, the separation tank and the second-cycle reactor. It operates by measuring the pressure in the outlet pipe of the “second- cycle transesterification reactor 30.”
  • the constant-pressure control valve is installed in the outlet pipe the second-cycle reactor at one point only by holding the system pressure at a higher level than that of the methanol vapor mixture flowing into the first-cycle reactor at 1.0 bar-gauge (barg).
  • This component has the function of mixing the raw glycerin discharged from the bottom of the “continual raw glycerin separation and disposal tank 17” with the raw methyl esters coming out of the “second-cycle reactor 30” through the “control valve 20”.
  • methyl esters coming from second-cycle reactor will cause small amounts of glycerin to develop, this small portion of the glycerin can dissolve into the full amount of the biodiesel methyl esters because there are methanol and soap that constitute a side reaction, mixing in with both the raw glycerin and raw methyl esters, preventing the present amount of raw glycerin from separating out from the raw biodiesel methyl esters.
  • the raw-glycerin mass When the raw-glycerin mass is mixed with the mixture flowing out from the second-cycle reactor, it will enable the newly formed glycerin to combine together and to separate out from the raw biodiesel methyl esters in the “continually operating separation tank of raw glycerin from raw methyl esters 22.”
  • “Continually operating separation tank of raw glycerin from raw methyl esters 22” The size of this tank is large, with a height of at least 10 meters and a tank diameter with an inflow and outflow capacity of at least 24 hours. The height of this tank will assist the flow of the raw biodiesel methyl esters flowing in to separate the raw glycerin so that it can accumulate on the bottom of the tank. Also, the raw biodiesel methyl esters will flow up onto the topside of the tank from the center of the tank, which will be at a high temperature. It will flow profusely out of the tank through the pipe and the tank will receive it in an amount equal to the amount of raw methyl esters continually flowing into the tank.
  • a beneficial natural phenomenon will have occurred, namely, that the interior surface of the tank, because of the tank’s large capacity, drains much of the heat away into the outer atmosphere, causing the temperature of the raw biodiesel methyl esters at the side of the tank to drop below the center of the tank and thereby causing the density of the raw biodiesel methyl esters at the side of the tank to be greater than the density of the raw biodiesel methyl esters at the center of the tank.
  • the raw biodiesel methyl esters are thus forced to circulate in a rotating pattern, spiraling down from the central upper tank surface downward toward the lower side within the inner surface of the tank.
  • This component generates the separation of the raw glycerin and raw biodiesel methyl esters. It is designed as shown in Figure 2. It will be a fishbone pipe and have a main feed pipe with a diameter that can be as much as four times larger than the pipe receiving the outflow mixture from the “fixed-blade mixing pipe 21,” making it possible to reduce the flow rate of the mixture extensively and to separate the flow to the fishbone sub-pipe.
  • This sub-pipe will have the same size as the pipe receiving the outflow mixture from the “fixed-blade mixing pipe 21,” which is connected to six symmetrical flow pipes at the open end of each of the six pipes. It will be placed along the circumference of a circle with a radius of no more than two meters in such a way that the flow will slowly rise from below to the top from the middle of the tank.
  • This component is used to gauge the level of the bond between the raw methyl esters and raw glycerin in the “continually operating separation tank of raw glycerin from raw methyl esters 22” through a display in the control system indicating the bond level of the layer of raw glycerin and raw biodiesel methyl esters.
  • This component consists of a pipe draining the raw methyl esters out from tank number 22, allowing the methyl esters to flow freely by use of a pipe as many as four times larger than the inlet pipe.
  • the purpose of this arrangement is to avoid disturbing the vertical swirling flow of the liquid in the “continually operating separation tank of raw glycerin from raw methyl esters 22.”
  • This unit consists of an evaporative vent pipe of hot methanol in the gap between the top side of the “continually operating separation tank of raw glycerin from raw methyl esters 22” and “the methyl ester receiving tank 27.” Its purpose is to control the pumping of the raw biodiesel methyl esters transmitted into the next production process without causing a pressure on the upper side of the “continually operating separation tank of raw glycerin from raw methyl esters 22,” to be lower than the vacuum which would cause the tank to cave in. The excess methanol vapor can be vented out from the cap of the “continually operating separation tank of raw glycerin from raw methyl esters 22,” thus keeping the pressure on the top side of the tank stable.
  • This tank is used to hold the methyl esters overflowing from the “continually operating separation tank of raw glycerin from raw methyl esters 22.”
  • the purpose is to enable a continual pumping of raw biodiesel methyl esters transmitted into a subsequent process of purging out contaminants from the biodiesel.
  • “Glycerin discharge pump 28” This unit has a function of pumping the raw glycerin out from the bottom of the “continually operating separation tank of raw glycerin from raw methyl esters 22” in order to deliver the raw glycerin into a subsequent soap removal process.
  • This unit has a structure and operates like the “first-cycle transesterification reactor 1” in every aspect.
  • the essential function of this second-cycle transesterification reactor is to carry out the transesterification reaction in order to derive methyl esters containing less than 0.3% monoglycerides.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne la mise au point d'un procédé et d'une application de séparation d'ester méthylique et de glycérine pour la production de biodiesel de grande pureté, qui implique plusieurs machines, équipements et processus. Après une réaction rapide de premier cycle, par une réduction du débit, la glycérine brute peut se séparer de la masse brute d'ester méthylique sous la forme de petites pastilles. La glycérine brute peut être forcée à subir d'autres cycles dans un mélange homogène avec le nouvel ester méthylique de biodiesel pendant au moins quatre cycles. Il est possible d'accélérer la poursuite de la réaction de transestérification jusqu'à ce que le niveau de qualité des esters méthyliques atteigne 96,5% au moyen du réacteur de premier cycle. Ensuite, à l'aide du réacteur de deuxième cycle, on obtiendra un niveau de qualité de 98% en ajoutant 5,0% de méthanol en poids par rapport au débit entrant dans le système, et 0,5% de méthylate de sodium d'huile de palme pure raffinée, respectivement.
PCT/TH2023/050006 2023-03-28 2023-03-28 Procédé et application de séparation d'ester méthylique et de glycérine utilisés dans un procédé de purification de biodiesel Pending WO2024205513A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/TH2023/050006 WO2024205513A1 (fr) 2023-03-28 2023-03-28 Procédé et application de séparation d'ester méthylique et de glycérine utilisés dans un procédé de purification de biodiesel

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/TH2023/050006 WO2024205513A1 (fr) 2023-03-28 2023-03-28 Procédé et application de séparation d'ester méthylique et de glycérine utilisés dans un procédé de purification de biodiesel

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WO2024205513A1 true WO2024205513A1 (fr) 2024-10-03

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PCT/TH2023/050006 Pending WO2024205513A1 (fr) 2023-03-28 2023-03-28 Procédé et application de séparation d'ester méthylique et de glycérine utilisés dans un procédé de purification de biodiesel

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070175092A1 (en) * 2005-11-28 2007-08-02 Ames Randall S Continuous flow biodiesel processor
WO2008122812A2 (fr) * 2007-04-10 2008-10-16 Nitech Solutions Limited Appareil et procédé de mélange tubulaire
US20090069586A1 (en) * 2005-02-21 2009-03-12 Nippon Shokubai Co., Ltd. Method for producing fatty acid alkyl esters and/or glycerin
WO2009039151A1 (fr) * 2007-09-19 2009-03-26 Best Energies, Inc. Procédé de fabrication de biodiesel à point de trouble réduit
US20110166378A1 (en) * 2003-03-20 2011-07-07 Pelly Michael F Method and apparatus for refining biodiesel
US9446366B2 (en) * 2011-10-04 2016-09-20 Brunel University Modular flow reactor

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20110166378A1 (en) * 2003-03-20 2011-07-07 Pelly Michael F Method and apparatus for refining biodiesel
US20090069586A1 (en) * 2005-02-21 2009-03-12 Nippon Shokubai Co., Ltd. Method for producing fatty acid alkyl esters and/or glycerin
US20070175092A1 (en) * 2005-11-28 2007-08-02 Ames Randall S Continuous flow biodiesel processor
WO2008122812A2 (fr) * 2007-04-10 2008-10-16 Nitech Solutions Limited Appareil et procédé de mélange tubulaire
WO2009039151A1 (fr) * 2007-09-19 2009-03-26 Best Energies, Inc. Procédé de fabrication de biodiesel à point de trouble réduit
US9446366B2 (en) * 2011-10-04 2016-09-20 Brunel University Modular flow reactor

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