CN110591818A - Production method of biodiesel fatty acid methyl ester with minus 20 ℃ and low condensation point - Google Patents
Production method of biodiesel fatty acid methyl ester with minus 20 ℃ and low condensation point Download PDFInfo
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- CN110591818A CN110591818A CN201910868149.4A CN201910868149A CN110591818A CN 110591818 A CN110591818 A CN 110591818A CN 201910868149 A CN201910868149 A CN 201910868149A CN 110591818 A CN110591818 A CN 110591818A
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- 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, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
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Abstract
The invention discloses a method for producing biodiesel fatty acid methyl ester with a freezing point of-20 ℃ and low freezing point, which comprises the operation of rectifying and separating biodiesel fatty acid methyl ester firstly and then separating biodiesel C18 fatty acid methyl ester, wherein when cooling water is introduced for cooling, the traditional two steps are changed into the existing three-step mode, this can avoid impurity after cooling which may occur too fast in temperature reduction in the conventional cooling process, thereby better cooling can be carried out, and the stirring speed is different, so that the stirring is more uniform, the reaction is more sufficient, the better cooling can be carried out, thereby solving the problem that impurities can be generated due to the rapid temperature reduction when the temperature of the fractionation kettle is reduced by the existing fatty acid methyl ester production method.
Description
Technical Field
The invention belongs to the technical field related to the synthesis of high molecular polymers, and particularly relates to a production method of biodiesel fatty acid methyl ester with a condensation point of-20 ℃.
Background
The fatty acid methyl ester is formed by methylation of fatty acid. Biodiesel is mainly composed of fatty acid methyl esters. In biochemistry, in order to analyze the content of various fatty acids in a sample, lipids in the sample are extracted, the sample is modified into FAMEs by a methylating agent such as BSTFA, the FAMEs can be separated, the content is measured, the isotopic abundance is judged and the like by a gas chromatography, and fatty acid methyl esters can be divided into unsaturated fatty acid methyl esters containing double bonds and saturated fatty acid methyl esters containing no double bonds or triple bonds according to the saturation degree of a carbon chain. The main use of saturated fatty acid methyl esters is the production of the aforementioned surfactants. The unsaturated fatty acid methyl ester can be used for producing the epoxy fatty acid methyl ester besides the surfactant. The latter is an important plasticizer, is widely used for plasticizing resins such as polyvinyl chloride and the like, and can partially replace phthalate plasticizers.
The prior art for producing fatty acid methyl ester has the following problems: when the temperature of a fractionation kettle is reduced in the conventional fatty acid methyl ester production method, the temperature may be reduced too fast, so that incomplete and sufficient reaction in the raw materials may occur, and the cooled materials may be impure, so that the raw materials are wasted and the problem of resource waste is caused.
Disclosure of Invention
The invention aims to provide a production method of biodiesel fatty acid methyl ester with a freezing point of 20 ℃ below zero, which aims to solve the problem that impurities can be generated due to the rapid temperature reduction when the temperature of a fractionation kettle is reduced in the conventional fatty acid methyl ester production method proposed in the background art.
In order to achieve the purpose, the invention provides the following technical scheme:
a production method of biodiesel fatty acid methyl ester with a temperature of-20 ℃ and a low condensation point comprises the following operation steps of rectification and separation of the biodiesel fatty acid methyl ester:
the method comprises the following steps: preparing raw materials, wherein the raw materials are biodiesel, the acid value is within 0.5mgKOH/g, no water or impurities are used as main raw materials, and a catalyst is not required to be prepared;
step two: the process of eliminating water, salt and solid impurity from crude oil by electrochemical separation or heating deposition. The main purpose is to prevent the salt from dissociating to generate hydrogen chloride to corrode equipment and prevent the salt scale from depositing in the tube furnace tube of the tube furnace. When electrochemical separation is adopted, several to dozens of ppm demulsifiers (ionic demulsifiers or nonionic polyether demulsifiers) and softened water are added into crude oil, and then salt-containing water drops are gathered and settled through a high-voltage electric field (the electric field intensity is 1.2-1.5 kV/cm), so that salt, water and other impurities in the crude oil are removed. Electrochemical desalination is often used in series with two sets of equipment to improve the desalination effect;
step three: switching on a power switch, and then starting a vacuum system and a pipeline until the vacuum degree in the tower is less than 50;
step four: then, the biodiesel is subjected to heat exchange work through a heat exchanger, and after the biodiesel is fully heated, the biodiesel is introduced into the interior of the gas evolution tank, so that trace gas impurities can be separated out under the action of the gas evolution tank;
step five: and heating the gas-separated biodiesel in the third step to enter a C16 rectifying tower, wherein the vacuum degree of the tower top is 50-60 Pa, the low vacuum degree of the tower is 150-180 Pa, and the temperature of the tower bottom is 160-180 ℃ to obtain the fatty acid methyl ester. Cooling distillates in the top of the rectifying tower and the rectifying tower: the front fraction fatty acid methyl ester and the middle fraction fatty acid methyl ester are C16 fatty acid methyl ester, and the reflux ratio of the tower top and the tower middle is 1.0: 1-2.0: 1;
step six: then heating the gas-separated biodiesel into a C16 rectifying tower, and vacuumizing the tower top: 50 to 60Pa, tower bottom temperature of 150 to 180Pa lower and fatty acid methyl ester of 160 to 180 degrees. The temperature of the top of the tower is controlled at 160 ℃ for 170 ℃ for 160 ℃ for 170 ℃, the reflux ratio of the top of the tower to the middle of the tower is 1.0: 1-2.0: 1, and distillates at the top of the rectifying tower and in the rectifying tower are cooled: front fraction fatty acid methyl ester (by-product), middle fraction C16 fatty acid methyl ester, C16 fatty acid methyl ester as by-product;
step seven: and (3) enabling the bottom residue biodiesel to enter a C18 rectifying tower through a heater, and vacuumizing the tower top: 50 to 60Pa, tower bottom temperature of 150 to 180Pa lower, and fatty acid methyl ester of 200 to 230 ℃. The temperature of the top of the tower is controlled at 175 ℃ for 160-year heating, the temperature of the middle of the tower is controlled at 190-year heating, the reflux ratio of the top of the tower to the middle of the tower is 1.0: 1-2.0: 1, and distillates at the top of the rectifying tower and in the rectifying tower are cooled: the front cut fatty acid methyl ester and the middle cut fatty acid methyl ester are C18. And cooling the bottom kettle liquid byproduct, feeding the cooled bottom kettle liquid byproduct into a kettle liquid storage tank, and waiting for fractionation of the main product biodiesel C18 fatty acid methyl ester.
Preferably, the operation steps of the biodiesel C18 fatty acid methyl ester fractionation are as follows:
the method comprises the following steps: preparing raw material biodiesel C18 fatty acid methyl ester, wherein the index of the raw material biodiesel C18 fatty acid methyl ester is within 0.5mgKOH/g of acid value, and the raw material biodiesel C18 fatty acid methyl ester is anhydrous, impurity-free, colorless and odorless and is used as a main raw material without preparing a catalyst;
step two: controlling the temperature of biodiesel (C18 fatty acid methyl ester) at 20-25 ℃ through a cooler, pumping the biodiesel into a fractionation kettle, starting a refrigerator and starting cooling water;
step three: pumping into a fractionation kettle, and cooling with chilled water. Reducing the temperature by 2-5 ℃ per hour, controlling the stirring speed at 60-80 rpm, slowly slowing the stirring speed along with the lapse of time by the control method, and reducing the temperature to 8-10 ℃;
step four: pumping into a fractionation kettle, and cooling with chilled water. Reducing the temperature by 1-3 ℃ per hour, controlling the stirring speed at 50-60 rpm, slowly slowing the stirring speed along with the lapse of time, and reducing the temperature to 2-6 ℃;
step five: pumping into a fractionation kettle, and cooling with chilled water. Reducing the temperature by 0.5-2 ℃ per hour, controlling the stirring speed at 40-60 r/min, slowly slowing down the stirring speed along with the lapse of time by the control method, reducing the temperature to-10-0 ℃, forming a good biodiesel crystal mixture by the biodiesel (C18 fatty acid methyl ester) after several hours, and waiting for filtration;
step six: pumping the biodiesel crystal mixture in the fractionation kettle into a plate and frame filter press, and filter-pressing filtrate, wherein the filtrate is a biodiesel (fatty acid methyl ester) product with a low condensation point of-20 ℃, and the filter cake is a methyl stearate byproduct;
step seven: the biodiesel (fatty acid methyl ester) product with the freezing point of 20 ℃ below zero can be widely applied to cold regions because the freezing point is below-20 ℃ and the cold filter plugging point is below-6 ℃ through detection.
Compared with the prior art, the invention provides a production method of biodiesel fatty acid methyl ester with a freezing point of-20 ℃, which has the following beneficial effects:
according to the invention, when cooling water is introduced for cooling, the traditional two steps are changed into the traditional three-step mode, so that the phenomenon of impurity after cooling due to too fast temperature reduction in the traditional cooling process can be avoided, the better cooling can be realized, and the stirring speed is different, so that the stirring is more uniform, the more sufficient reaction can be realized, the better cooling can be realized, and the problem that impurity can be caused due to too fast temperature reduction in the temperature reduction of the fractionation kettle in the traditional fatty acid methyl ester production method can be solved.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be obtained by a person skilled in the art without any inventive step based on the embodiments of the present invention, are within the scope of the present invention.
The invention provides a technical scheme that:
a production method of biodiesel fatty acid methyl ester with a temperature of minus 20 ℃ and a low condensation point comprises the following operation steps of rectification and separation of the biodiesel fatty acid methyl ester:
the method comprises the following steps: preparing raw materials, wherein the raw materials are biodiesel, the acid value is within 0.5mgKOH/g, no water or impurities are used as main raw materials, and a catalyst is not required to be prepared;
step two: the process of eliminating water, salt and solid impurity from crude oil by electrochemical separation or heating deposition. The main purpose is to prevent the salt from dissociating to generate hydrogen chloride to corrode equipment and prevent the salt scale from depositing in the tube furnace tube of the tube furnace. When electrochemical separation is adopted, several to dozens of ppm demulsifiers (ionic demulsifiers or nonionic polyether demulsifiers) and softened water are added into crude oil, and then salt-containing water drops are gathered and settled through a high-voltage electric field (the electric field intensity is 1.2-1.5 kV/cm), so that salt, water and other impurities in the crude oil are removed. Electrochemical desalination is often used in series with two sets of equipment to improve the desalination effect;
step three: switching on a power switch, and then starting a vacuum system and a pipeline until the vacuum degree in the tower is less than 50;
step four: then, the biodiesel is subjected to heat exchange work through a heat exchanger, and after the biodiesel is fully heated, the biodiesel is introduced into the interior of the gas evolution tank, so that trace gas impurities can be separated out under the action of the gas evolution tank;
step five: and heating the gas-separated biodiesel in the third step to enter a C16 rectifying tower, wherein the vacuum degree of the tower top is 50-60 Pa, the low vacuum degree of the tower is 150-180 Pa, and the temperature of the tower bottom is 160-180 ℃ to obtain the fatty acid methyl ester. Cooling distillates in the top of the rectifying tower and the rectifying tower: the front fraction fatty acid methyl ester and the middle fraction fatty acid methyl ester are C16 fatty acid methyl ester, and the reflux ratio of the tower top and the tower middle is 1.0: 1-2.0: 1;
step six: then heating the gas-separated biodiesel into a C16 rectifying tower, and vacuumizing the tower top: 50 to 60Pa, tower bottom temperature of 150 to 180Pa lower and fatty acid methyl ester of 160 to 180 degrees. The temperature of the top of the tower is controlled at 160 ℃ for 170 ℃ for 160 ℃ for 170 ℃, the reflux ratio of the top of the tower to the middle of the tower is 1.0: 1-2.0: 1, and distillates at the top of the rectifying tower and in the rectifying tower are cooled: front fraction fatty acid methyl ester (by-product), middle fraction C16 fatty acid methyl ester, C16 fatty acid methyl ester as by-product;
step seven: and (3) enabling the bottom residue biodiesel to enter a C18 rectifying tower through a heater, and vacuumizing the tower top: 50 to 60Pa, tower bottom temperature of 150 to 180Pa lower, and fatty acid methyl ester of 200 to 230 ℃. The temperature of the top of the tower is controlled at 175 ℃ for 160-year heating, the temperature of the middle of the tower is controlled at 190-year heating, the reflux ratio of the top of the tower to the middle of the tower is 1.0: 1-2.0: 1, and distillates at the top of the rectifying tower and in the rectifying tower are cooled: the front cut fatty acid methyl ester and the middle cut fatty acid methyl ester are C18. And cooling the bottom kettle liquid byproduct, feeding the cooled bottom kettle liquid byproduct into a kettle liquid storage tank, and waiting for fractionation of the main product biodiesel C18 fatty acid methyl ester.
The operating steps of the biodiesel C18 fatty acid methyl ester fractionation are as follows:
the method comprises the following steps: preparing raw material biodiesel C18 fatty acid methyl ester, wherein the index of the raw material biodiesel C18 fatty acid methyl ester is within 0.5mgKOH/g of acid value, and the raw material biodiesel C18 fatty acid methyl ester is anhydrous, impurity-free, colorless and odorless and is used as a main raw material without preparing a catalyst;
step two: controlling the temperature of biodiesel (C18 fatty acid methyl ester) at 20-25 ℃ through a cooler, pumping the biodiesel into a fractionation kettle, starting a refrigerator and starting cooling water;
step three: pumping into a fractionation kettle, and cooling with chilled water. Reducing the temperature by 2-5 ℃ per hour, controlling the stirring speed at 60-80 rpm, slowly slowing the stirring speed along with the lapse of time by the control method, and reducing the temperature to 8-10 ℃;
step four: pumping into a fractionation kettle, and cooling with chilled water. Reducing the temperature by 1-3 ℃ per hour, controlling the stirring speed at 50-60 rpm, slowly slowing the stirring speed along with the lapse of time, and reducing the temperature to 2-6 ℃;
step five: pumping into a fractionation kettle, and cooling with chilled water. Reducing the temperature by 0.5-2 ℃ per hour, controlling the stirring speed at 40-60 r/min, slowly slowing down the stirring speed along with the lapse of time by the control method, reducing the temperature to-10-0 ℃, forming a good biodiesel crystal mixture by the biodiesel (C18 fatty acid methyl ester) after several hours, and waiting for filtration;
step six: pumping the biodiesel crystal mixture in the fractionation kettle into a plate and frame filter press, and filter-pressing filtrate, wherein the filtrate is a biodiesel (fatty acid methyl ester) product with a low condensation point of-20 ℃, and the filter cake is a methyl stearate byproduct;
step seven: the biodiesel (fatty acid methyl ester) product with the freezing point of 20 ℃ below zero can be widely applied to cold regions because the freezing point is below-20 ℃ and the cold filter plugging point is below-6 ℃ through detection.
The working principle and the using process of the invention are as follows:
the method comprises the following steps: switching on a power switch, and then starting a vacuum system and a pipeline until the vacuum degree in the tower is less than 50;
step two: then, the biodiesel is subjected to heat exchange work through a heat exchanger, and after the biodiesel is fully heated, the biodiesel is introduced into the interior of the gas evolution tank, so that trace gas impurities can be separated out under the action of the gas evolution tank;
step three: and heating the gas-separated biodiesel in the second step into a C16 rectifying tower, wherein the vacuum degree of the tower top is 50-60 Pa, the low vacuum degree of the tower is 150-180 Pa, and the temperature of the tower bottom is 160-180 ℃ to obtain the fatty acid methyl ester. Cooling distillates in the top of the rectifying tower and the rectifying tower: the front fraction fatty acid methyl ester and the middle fraction fatty acid methyl ester are C16 fatty acid methyl ester, and the reflux ratio of the tower top and the tower middle is 1.0: 1-2.0: 1;
step four: then heating the gas-separated biodiesel into a C16 rectifying tower, and vacuumizing the tower top: 50 to 60Pa, tower bottom temperature of 150 to 180Pa lower and fatty acid methyl ester of 160 to 180 degrees. The temperature of the top of the tower is controlled at 160 ℃ for 170 ℃ for 160 ℃ for 170 ℃, the reflux ratio of the top of the tower to the middle of the tower is 1.0: 1-2.0: 1, and distillates at the top of the rectifying tower and in the rectifying tower are cooled: front fraction fatty acid methyl ester (by-product), middle fraction C16 fatty acid methyl ester, C16 fatty acid methyl ester as by-product;
step five: and (3) enabling the bottom residue biodiesel to enter a C18 rectifying tower through a heater, and vacuumizing the tower top: 50 to 60Pa, tower bottom temperature of 150 to 180Pa lower, and fatty acid methyl ester of 200 to 230 ℃. The temperature of the top of the tower is controlled at 175 ℃ for 160-year heating, the temperature of the middle of the tower is controlled at 190-year heating, the reflux ratio of the top of the tower to the middle of the tower is 1.0: 1-2.0: 1, and distillates at the top of the rectifying tower and in the rectifying tower are cooled: the front cut fatty acid methyl ester and the middle cut fatty acid methyl ester are C18. And cooling the bottom kettle liquid byproduct, feeding the cooled bottom kettle liquid byproduct into a kettle liquid storage tank, and waiting for fractionation of the main product biodiesel C18 fatty acid methyl ester.
The operating steps of the biodiesel C18 fatty acid methyl ester fractionation are as follows:
the method comprises the following steps: preparing raw material biodiesel C18 fatty acid methyl ester, wherein the index of the raw material biodiesel C18 fatty acid methyl ester is within 0.5mgKOH/g of acid value, and the raw material biodiesel C18 fatty acid methyl ester is anhydrous, impurity-free, colorless and odorless and is used as a main raw material without preparing a catalyst;
step two: controlling the temperature of biodiesel (C18 fatty acid methyl ester) at 20-25 ℃ through a cooler, pumping the biodiesel into a fractionation kettle, starting a refrigerator and starting cooling water;
step three: pumping into a fractionation kettle, and cooling with chilled water. Reducing the temperature by 2-5 ℃ per hour, controlling the stirring speed at 60-80 rpm, slowly slowing the stirring speed along with the lapse of time by the control method, and reducing the temperature to 8-10 ℃;
step four: pumping into a fractionation kettle, and cooling with chilled water. Reducing the temperature by 1-3 ℃ per hour, controlling the stirring speed at 50-60 rpm, slowly slowing the stirring speed along with the lapse of time, and reducing the temperature to 2-6 ℃;
step five: pumping into a fractionation kettle, and cooling with chilled water. Reducing the temperature by 0.5-2 ℃ per hour, controlling the stirring speed at 40-60 r/min, slowly slowing down the stirring speed along with the lapse of time by the control method, reducing the temperature to-10-0 ℃, forming a good biodiesel crystal mixture by the biodiesel (C18 fatty acid methyl ester) after several hours, and waiting for filtration;
step six: pumping the biodiesel crystal mixture in the fractionation kettle into a plate and frame filter press, and filter-pressing filtrate, wherein the filtrate is a biodiesel (fatty acid methyl ester) product with a low condensation point of-20 ℃, and the filter cake is a methyl stearate byproduct;
step seven: the biodiesel (fatty acid methyl ester) product with the freezing point of 20 ℃ below zero can be widely applied to cold regions because the freezing point is below-20 ℃ and the cold filter plugging point is below-6 ℃ through detection.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (2)
1. A production method of biodiesel fatty acid methyl ester with a temperature of-20 ℃ and a low condensation point is characterized by comprising the following steps: the operation steps of the rectification separation of the biodiesel fatty acid methyl ester are as follows:
the method comprises the following steps: preparing raw materials, wherein the raw materials are biodiesel, the acid value is within 0.5mgKOH/g, no water or impurities are used as main raw materials, and a catalyst is not required to be prepared;
step two: the process of eliminating water, salt and solid impurity from crude oil by electrochemical separation or heating deposition process. The main purpose is to prevent the salt from dissociating to generate hydrogen chloride to corrode equipment and prevent the salt scale from depositing in the tube furnace tube of the tube furnace. When electrochemical separation is adopted, several to dozens of ppm demulsifiers (ionic demulsifiers or nonionic polyether demulsifiers) and softened water are added into crude oil, and then salt-containing water drops are aggregated and settled through a high-voltage electric field (the electric field intensity is 1.2-1.5 kV/cm), so that salt, water and other impurities in the crude oil are removed. Electrochemical desalination is often used in series with two sets of equipment to improve the desalination effect;
step three: switching on a power switch, and then starting a vacuum system and a pipeline until the vacuum degree in the tower is within 50;
step four: then, the biodiesel is subjected to heat exchange work through a heat exchanger, and after the biodiesel is fully heated, the biodiesel is introduced into the interior of the gas evolution tank, so that trace gas impurities can be separated out under the action of the gas evolution tank;
step five: and heating the gas-separated biodiesel in the third step to enter a C16 rectifying tower, wherein the vacuum degree of the tower top is 50-60 Pa, the low vacuum degree of the tower is 150-180 Pa, and the temperature of the tower bottom is 160-180 ℃ to obtain the fatty acid methyl ester. Cooling distillates in the top of the rectifying tower and the rectifying tower: the front fraction fatty acid methyl ester and the middle fraction are C16 fatty acid methyl ester, and the reflux ratio of the tower top and the tower middle is 1.0: 1-2.0: 1;
step six: then heating the gas-separated biodiesel into a C16 rectifying tower, and vacuumizing the tower top: 50 to 60Pa, tower bottom temperature of 150 to 180Pa lower and fatty acid methyl ester of 160 to 180 degrees. The temperature of the tower top is controlled at 160 ℃ and 160 ℃ respectively, the temperature of the tower is controlled at 170 ℃ and 160 ℃ respectively, the reflux ratio of the tower top to the tower middle is 1.0: 1-2.0: 1, and distillates at the tower top and the rectifying tower are cooled: front cut fatty acid methyl ester (by-product), middle cut is C16 fatty acid methyl ester, C16 fatty acid methyl ester is by-product;
step seven: and (3) enabling the bottom residue biodiesel to enter a C18 rectifying tower through a heater, and vacuumizing the tower top: 50 to 60Pa, tower bottom temperature of 150 to 180Pa lower, and fatty acid methyl ester of 200 to 230 ℃. The temperature of the tower top is controlled at 175 ℃ and the temperature of the tower is controlled at 190 ℃ and the reflux ratio of the tower top and the tower is 1.0: 1-2.0: 1, and distillates at the tower top and the rectifying tower are cooled: the front fraction fatty acid methyl ester and the middle fraction fatty acid methyl ester are C18. And cooling the bottom kettle liquid byproduct to enter a kettle liquid storage tank, and waiting for fractionation of the main product biodiesel C18 fatty acid methyl ester.
2. The method for producing biodiesel fatty acid methyl ester with low freezing point of-20 ℃ according to claim 1, wherein the production method comprises the following steps: the operating steps of the biodiesel C18 fatty acid methyl ester fractionation are as follows:
the method comprises the following steps: preparing raw material biodiesel C18 fatty acid methyl ester, wherein the index of the raw material biodiesel C18 fatty acid methyl ester is within 0.5mgKOH/g of acid value, and the raw material biodiesel C18 fatty acid methyl ester is anhydrous, impurity-free, colorless and odorless and is used as a main raw material without preparing a catalyst;
step two: controlling the temperature of biodiesel (C18 fatty acid methyl ester) at 20-25 ℃ through a cooler, pumping the biodiesel into a fractionation kettle, starting a refrigerator and starting cooling water;
step three: pumping into a fractionation kettle, and cooling with chilled water. Reducing the temperature by 2-5 ℃ per hour, controlling the stirring speed at 60-80 rpm, slowly slowing the stirring speed along with the lapse of time, and reducing the temperature to 8-10 ℃;
step four: pumping into a fractionation kettle, and cooling with chilled water. Reducing the temperature by 1-3 ℃ per hour, controlling the stirring speed at 50-60 rpm, slowly slowing the stirring speed along with the lapse of time, and reducing the temperature to 2-6 ℃;
step five: pumping into a fractionation kettle, and cooling with chilled water. Reducing the temperature by 0.5-2 ℃ per hour, controlling the stirring speed at 40-60 r/min, slowly slowing down the stirring speed along with the lapse of time by the control method, reducing the temperature to-10-0 ℃, forming a good biodiesel crystal mixture by biodiesel (C18 fatty acid methyl ester) after several hours, and waiting for filtration;
step six: pumping the biodiesel crystal mixture in the fractionation kettle into a plate and frame filter press, and filter-pressing filtrate, wherein the filtrate is a biodiesel (fatty acid methyl ester) product with a low condensation point of-20 ℃, and the filter cake is a methyl stearate byproduct;
step seven: the biodiesel (fatty acid methyl ester) product with the freezing point of 20 ℃ below zero can be widely applied to cold regions because the freezing point is below-20 ℃ and the cold filter plugging point is below-6 ℃ through detection.
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| GB2608744A (en) * | 2020-09-25 | 2023-01-11 | Abundia Biomass To Liquids Ltd | Converting biomass to diesel |
| GB2608745A (en) * | 2020-09-25 | 2023-01-11 | Abundia Biomass To Liquids Ltd | Converting biomass to naphtha |
| GB2608923A (en) * | 2020-09-25 | 2023-01-18 | Abundia Biomass To Liquids Ltd | Converting biomass to LPG |
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| GB2608744A (en) * | 2020-09-25 | 2023-01-11 | Abundia Biomass To Liquids Ltd | Converting biomass to diesel |
| GB2608745A (en) * | 2020-09-25 | 2023-01-11 | Abundia Biomass To Liquids Ltd | Converting biomass to naphtha |
| GB2608923A (en) * | 2020-09-25 | 2023-01-18 | Abundia Biomass To Liquids Ltd | Converting biomass to LPG |
| GB2609115A (en) * | 2020-09-25 | 2023-01-25 | Abundia Biomass To Liquids Ltd | Converting biomass to jet-fuel |
| CN114214121A (en) * | 2021-12-14 | 2022-03-22 | 浙江东江能源科技有限公司 | High-quality low-sulfur-content biodiesel preparation device and preparation method |
| CN114214121B (en) * | 2021-12-14 | 2024-02-20 | 浙江东江能源科技有限公司 | Preparation device and preparation method of high-quality low-sulfur biodiesel |
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