CN112852552A - Method for preparing bunker fuel oil by using illegal cooking oil based on glycerol esterification process - Google Patents
Method for preparing bunker fuel oil by using illegal cooking oil based on glycerol esterification process Download PDFInfo
- Publication number
- CN112852552A CN112852552A CN202110099292.9A CN202110099292A CN112852552A CN 112852552 A CN112852552 A CN 112852552A CN 202110099292 A CN202110099292 A CN 202110099292A CN 112852552 A CN112852552 A CN 112852552A
- Authority
- CN
- China
- Prior art keywords
- glycerol
- reaction
- oil
- product
- fatty acid
- 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
Links
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
- C11C3/04—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fats or fatty oils
- C11C3/06—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fats or fatty oils with glycerol
-
- 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, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
-
- 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
- C11C1/00—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids
- C11C1/08—Refining
-
- 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
- C11C1/00—Preparation of fatty acids from fats, fatty oils, or waxes; Refining the fatty acids
- C11C1/08—Refining
- C11C1/10—Refining by distillation
-
- 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
- C11C3/04—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fats or fatty oils
- C11C3/10—Ester interchange
Abstract
The invention relates to a method for preparing bunker fuel oil by using illegal cooking oil based on a glycerol esterification process, which comprises the following steps: preheating raw oil and filtering solid impurities to obtain liquid crude oil, pumping the liquid crude oil and glycerol into a reaction pipe in proportion, enabling the liquid crude oil and the glycerol to carry out glycerol esterification reaction in the reaction pipe, cooling a product of the glycerol esterification reaction through a heat exchanger, injecting the product of the glycerol esterification reaction and methanol into a second reaction kettle in proportion to carry out ester exchange reaction, washing the product of the ester exchange reaction with water, carrying out centrifugal separation, introducing the centrifuged water-containing fatty acid methyl ester into a flash evaporation dryer to carry out dehydration, and decolorizing the dehydrated fatty acid methyl ester to obtain the purified combustion marine oil. The beneficial effects are that: the amount of solid impurities in the marine fuel oil is reduced, and the energy required by preheating the raw oil is reduced; the excessive methanol residue is avoided; the esterification reaction of the glycerol is thorough by reasonably preparing the amount of the glycerol, so that the acidity value is reduced.
Description
Technical Field
The invention relates to the field of biodiesel preparation, in particular to a method for preparing bunker fuel oil by using illegal cooking oil based on a glycerol esterification process.
Background
The illegal cooking oil is a general name of various inferior oils in life, has extremely poor quality and insanitation, and has serious overproof peroxide value, acid value and moisture. At present, the treatment of the 'illegal cooking oil' is mainly carried out by primary processing or simple deep processing, and the prepared products comprise: stearic acid raw material, feed additive, soap raw material, machining oil, demoulding oil and the like. All the methods have the same problems of technical lag, simple and crude equipment, serious pollution, bad sanitary condition and the like. The recycling of the illegal cooking oil is an effective way for restraining toxic oil.
The existing method for preparing biodiesel by using illegal cooking oil has the defects of more solid impurities, high energy consumption, high methanol residue and high acidity value, and is easy to cause engine corrosion.
Disclosure of Invention
The invention aims to overcome the problems in the prior art and provides a method for preparing bunker fuel oil by using illegal cooking oil based on a glycerol esterification process.
In order to achieve the technical purpose and achieve the technical effect, the invention is realized by the following technical scheme:
the method for preparing the marine fuel oil by using the illegal cooking oil based on the glycerol esterification process comprises the following steps:
s1, pouring the raw oil into a first reaction kettle provided with a heat exchanger and a filter screen, preheating the raw oil and filtering solid impurities to obtain liquid crude oil;
s2, pumping liquid crude oil and glycerol into a reaction tube in proportion, heating the reaction tube by using a heater at the same time, so that the liquid crude oil and the glycerol are subjected to glycerol esterification reaction in the reaction tube, and cooling the product of the glycerol esterification reaction through a heat exchanger;
s3, proportionally injecting the product of the glycerol esterification reaction and methanol into a second reaction kettle for ester exchange reaction;
s4, washing the product of the ester exchange reaction with water, then carrying out centrifugal separation, recovering glycerol to a glycerol storage tank for recycling, and introducing the centrifuged water-containing fatty acid methyl ester into a flash dryer for dehydration;
and S5, decoloring the dehydrated fatty acid methyl ester to obtain the purified marine combustion oil.
In the step S1, the raw oil preheating temperature is 100-120 ℃, so that water in the raw oil is evaporated, the water content in the raw oil is reduced, and the subsequent glycerol esterification reaction is facilitated.
In the step S1, the heat exchanger is located above the filter screen, and the filter screen and the heat exchanger are both inclined toward the slag discharge port of the first reaction vessel, so that the solid impurities in the feedstock oil enter the slag discharge port along the surface of the heat exchanger and the upper surface of the filter screen.
In step S2, the reaction tube is a spiral tube, a plurality of spiral turbulence blades are installed in the reaction tube, a plurality of heaters are installed outside the reaction tube, and the upper end of the reaction tube is communicated with the inlet end of the heat exchanger to cool the product of the glycerol esterification reaction through the heat exchanger.
In step S2, the molar ratio of glycerol to fatty acid in the liquid crude oil is 1:1-2:1, the temperature in the reaction tube changes in a gradient manner from 120 to 240 ℃ from bottom to top, and the glycerol and the liquid crude oil slowly flow in the reaction tube for 3 to 4 hours.
The temperature in the reaction tube is changed in a gradient manner, so that the glycerol esterification reaction of fatty acids with different chain lengths is facilitated, the glycerol esterification degree of the fatty acids is facilitated to be improved, and the acid value is reduced.
In the step S3, the mass of the methanol is 4-8% of that of the glycerol esterification product, KOH with the mass of the methanol being 0.5-2% of that of the glycerol esterification product is added, the reaction temperature in the second reaction kettle is 220-240 ℃, and the ester exchange time is 70-90 minutes.
In the step S4, pumping a product of the ester exchange reaction into a third reaction kettle, adding water with the mass of 5-10% of that of the product of the ester exchange reaction into the third reaction kettle, stirring and washing for 20 minutes at 45-55 ℃, injecting the mixture after washing into a disk centrifuge for centrifugal separation, recovering glycerol into a glycerol storage tank for recycling, and introducing the water-containing fatty acid methyl ester after centrifugation into a flash dryer for dehydration.
Step S5, adding fatty acid methyl ester into a fourth reaction kettle, adding activated clay which accounts for 5-9% of the mass of the fatty acid methyl ester and bentonite which accounts for 5-9% of the mass of the fatty acid methyl ester into the fourth reaction kettle, stirring for 1 hour at the temperature of 80-88 ℃, and then standing for 1 hour to obtain a supernatant; adding hydrogen peroxide accounting for 3-8% of the mass of the fatty acid methyl ester into the supernatant, stirring for 30 minutes at the temperature of 80-88 ℃, standing for 1 hour, and filtering to obtain the purified marine combustion oil.
The invention has the beneficial effects that: the product of the glycerol esterification reaction is cooled by a heat exchanger on one hand, and raw oil is preheated on the other hand, so that the raw oil is melted into a liquid state and then separated from solid impurities in the raw oil, the solid impurities are intercepted, and the solid impurities are further separated in the subsequent centrifugal process, thereby reducing the amount of the solid impurities in the marine fuel oil and reducing the energy required by preheating the raw oil; during the ester exchange reaction, methanol with a proper proportion is added, namely the methanol required by glyceride replacement is ensured, and the excessive residual quantity of the methanol caused by excessive methanol is avoided; the esterification reaction of the glycerol is thorough by reasonably preparing the amount of the glycerol, so that the acidity value is reduced.
Detailed Description
The present invention will be described in detail with reference to examples.
In one embodiment, a method for preparing bunker fuel oil from illegal cooking oil based on a glycerol esterification process comprises the following steps:
s1, pouring the raw oil into a first reaction kettle provided with a heat exchanger and a filter screen, wherein the heat exchanger is positioned above the filter screen, the filter screen and the heat exchanger are inclined towards the direction of a slag discharge port of the first reaction kettle, the raw oil is preheated to 100-120 ℃ by the heat exchanger, so that the liquid raw oil falls into the bottom of the first reaction kettle through the filter screen, solid impurities in the raw oil enter the slag discharge port along the surface of the heat exchanger and the upper surface of the filter screen, and the liquid raw oil is obtained by filtering the solid impurities;
s2, pumping liquid crude oil and glycerol into a reaction tube according to the molar ratio of 1:1 of the glycerol to fatty acid in the liquid crude oil, installing 6 heaters outside the reaction tube, enabling the temperature in the reaction tube to be changed in a gradient manner from 120-240 ℃ from bottom to top, namely enabling the reaction tube to form 6 temperature gradients from bottom to top, enabling the difference between two adjacent temperature gradients to be 20 ℃, enabling the glycerol and the liquid crude oil to slowly flow in the reaction tube for 3 hours, enabling the liquid crude oil and the glycerol to perform glycerol esterification reaction in the reaction tube, and enabling the upper end of the reaction tube to be communicated with the inlet end of a heat exchanger to cool a product of the glycerol esterification reaction through the heat exchanger;
s3, proportionally injecting the product of the glycerol esterification and methanol into a second reaction kettle for ester exchange reaction, wherein the mass of the methanol is 8% of that of the product of the glycerol esterification, and KOH with the mass of 2% of that of the product of the glycerol esterification is added, the reaction temperature in the second reaction kettle is 220-240 ℃, and the ester exchange time is 70 minutes;
s4, pumping a product of the ester exchange reaction into a third reaction kettle, adding water with the mass of 5% of that of the product of the ester exchange reaction into the third reaction kettle, stirring and washing for 20 minutes at 45-55 ℃, injecting the mixture after washing into a disk centrifuge for centrifugal separation, recovering glycerol into a glycerol storage tank for recycling, and introducing the water-containing fatty acid methyl ester after centrifugation into a flash dryer for dehydration;
s5, adding fatty acid methyl ester into a fourth reaction kettle, adding activated clay which accounts for 5% of the mass of the fatty acid methyl ester and bentonite which accounts for 9% of the mass of the fatty acid methyl ester into the fourth reaction kettle, stirring for 1 hour at the temperature of 80-88 ℃, standing for 1 hour, and taking supernatant; adding hydrogen peroxide accounting for 3% of the mass of the fatty acid methyl ester into the supernatant, stirring for 30 minutes at the temperature of 80-88 ℃, standing for 1 hour, and filtering to obtain the purified marine combustion oil.
In step S2, the reaction tube is a spiral tube, and a plurality of spiral turbulence blades are installed in the reaction tube.
The marine fuel oil produced in this example had an acid value of 0.5mgKOH/g as determined by the acid value determination method specified in GB/T14489.3-93, and had a methanol content of 0.2 as determined by gas chromatography.
Example two, a method for preparing bunker fuel oil using illegal cooking oil based on a glycerol esterification process, comprising:
s1, pouring the raw oil into a first reaction kettle provided with a heat exchanger and a filter screen, wherein the heat exchanger is positioned above the filter screen, the filter screen and the heat exchanger are inclined towards the direction of a slag discharge port of the first reaction kettle, the raw oil is preheated to 100-120 ℃ by the heat exchanger, so that the liquid raw oil falls into the bottom of the first reaction kettle through the filter screen, solid impurities in the raw oil enter the slag discharge port along the surface of the heat exchanger and the upper surface of the filter screen, and the liquid raw oil is obtained by filtering the solid impurities;
s2, pumping liquid crude oil and glycerol into a reaction tube according to the molar ratio of glycerol to fatty acid in the liquid crude oil of 1.5:1, installing 8 heaters outside the reaction tube, enabling the temperature in the reaction tube to change in a gradient manner from 120-240 ℃ from bottom to top, namely enabling the reaction tube to form 8 temperature gradients from bottom to top, enabling the difference between two adjacent temperature gradients to be 15 ℃, enabling the glycerol and the liquid crude oil to slowly flow in the reaction tube for 3.5 hours, enabling the liquid crude oil and the glycerol to carry out glycerol esterification reaction in the reaction tube, communicating the upper end of the reaction tube with the inlet end of a heat exchanger, and cooling a product of the glycerol esterification reaction through the heat exchanger;
s3, proportionally injecting the product of the glycerol esterification and methanol into a second reaction kettle for transesterification, wherein the mass of the methanol is 6% of that of the product of the glycerol esterification, KOH with the mass of 1% of that of the product of the glycerol esterification is added, the reaction temperature in the second reaction kettle is 220-240 ℃, and the transesterification time is 80 minutes;
s4, pumping a product of the ester exchange reaction into a third reaction kettle, adding water with the mass of 8% of that of the product of the ester exchange reaction into the third reaction kettle, stirring and washing for 20 minutes at 45-55 ℃, injecting the mixture after washing into a disk centrifuge for centrifugal separation, recovering glycerol into a glycerol storage tank for recycling, and introducing the water-containing fatty acid methyl ester after centrifugation into a flash dryer for dehydration;
s5, adding fatty acid methyl ester into a fourth reaction kettle, adding activated clay 7% of the mass of the fatty acid methyl ester and bentonite 5% of the mass of the fatty acid methyl ester into the fourth reaction kettle, stirring for 1 hour at the temperature of 80-88 ℃, and then standing for 1 hour to obtain a supernatant; adding hydrogen peroxide accounting for 5% of the mass of the fatty acid methyl ester into the supernatant, stirring for 30 minutes at the temperature of 80-88 ℃, standing for 1 hour, and filtering to obtain the purified marine combustion oil.
In step S2, the reaction tube is a spiral tube, and a plurality of spiral turbulence blades are installed in the reaction tube.
The marine fuel oil produced in the example had an acid value of 0.4mgKOH/g as determined by an acid value determination method specified in GB/T14489.3-93, and had a methanol content of 0.15 as determined by gas chromatography.
Example three, a method for preparing bunker fuel oil using illegal cooking oil based on a glycerol esterification process, comprising:
s1, pouring the raw oil into a first reaction kettle provided with a heat exchanger and a filter screen, wherein the heat exchanger is positioned above the filter screen, the filter screen and the heat exchanger are inclined towards the direction of a slag discharge port of the first reaction kettle, the raw oil is preheated to 100-120 ℃ by the heat exchanger, so that the liquid raw oil falls into the bottom of the first reaction kettle through the filter screen, solid impurities in the raw oil enter the slag discharge port along the surface of the heat exchanger and the upper surface of the filter screen, and the liquid raw oil is obtained by filtering the solid impurities;
s2, pumping liquid crude oil and glycerol into a reaction tube according to the molar ratio of 2:1 of the glycerol to fatty acid in the liquid crude oil, arranging 12 heaters outside the reaction tube, enabling the temperature in the reaction tube to be changed in a gradient manner from 120-240 ℃ from bottom to top, namely enabling the reaction tube to form 12 temperature gradients from bottom to top, enabling the difference between two adjacent temperature gradients to be 10 ℃, enabling the glycerol and the liquid crude oil to slowly flow in the reaction tube for 4 hours, enabling the liquid crude oil and the glycerol to carry out glycerol esterification reaction in the reaction tube, and enabling the upper end of the reaction tube to be communicated with the inlet end of a heat exchanger to cool a product of the glycerol esterification reaction through the heat exchanger;
s3, proportionally injecting the product of the glycerol esterification and methanol into a second reaction kettle for ester exchange reaction, wherein the mass of the methanol is 4% of that of the product of the glycerol esterification, KOH with the mass of 0.5% of that of the product of the glycerol esterification is added, the reaction temperature in the second reaction kettle is 55-65 ℃, and the ester exchange time is 90 minutes;
s4, pumping a product of the ester exchange reaction into a third reaction kettle, adding water with the mass of 5-10% of that of the product of the ester exchange reaction into the third reaction kettle, stirring and washing for 20 minutes at 45-55 ℃, injecting the washed mixture into a disc centrifuge for centrifugal separation, recovering glycerol into a glycerol storage tank for recycling, and introducing the centrifuged water-containing fatty acid methyl ester into a flash dryer for dehydration;
s5, adding fatty acid methyl ester into a fourth reaction kettle, adding activated clay 9% of the mass of the fatty acid methyl ester and bentonite 9% of the mass of the fatty acid methyl ester into the fourth reaction kettle, stirring for 1 hour at the temperature of 80-88 ℃, and then standing for 1 hour to obtain a supernatant; adding hydrogen peroxide accounting for 8% of the mass of the fatty acid methyl ester into the supernatant, stirring for 30 minutes at the temperature of 80-88 ℃, standing for 1 hour, and filtering to obtain the purified marine combustion oil.
In step S2, the reaction tube is a spiral tube, and a plurality of spiral turbulence blades are installed in the reaction tube.
The marine fuel oil produced in the example had an acid value of 0.4mgKOH/g as determined by an acid value determination method specified in GB/T14489.3-93, and had a methanol content of 0.1 as determined by gas chromatography.
In the description herein, references to the description of "one embodiment," "an example," "a specific example" or the like are intended to mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
The foregoing shows and describes the general principles, essential features, and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are described in the specification and illustrated only to illustrate the principle of the present invention, but that various changes and modifications may be made therein without departing from the spirit and scope of the present invention, which fall within the scope of the invention as claimed.
Claims (8)
1. The method for preparing the marine fuel oil by using the illegal cooking oil based on the glycerol esterification process is characterized by comprising the following steps of:
s1, pouring the raw oil into a first reaction kettle provided with a heat exchanger and a filter screen, preheating the raw oil and filtering solid impurities to obtain liquid crude oil;
s2, pumping liquid crude oil and glycerol into a reaction tube in proportion, heating the reaction tube by using a heater at the same time, so that the liquid crude oil and the glycerol are subjected to glycerol esterification reaction in the reaction tube, and cooling the product of the glycerol esterification reaction through a heat exchanger;
s3, proportionally injecting the product of the glycerol esterification reaction and methanol into a second reaction kettle for ester exchange reaction;
s4, washing the product of the ester exchange reaction with water, then carrying out centrifugal separation, recovering glycerol to a glycerol storage tank for recycling, and introducing the centrifuged water-containing fatty acid methyl ester into a flash dryer for dehydration;
and S5, decoloring the dehydrated fatty acid methyl ester to obtain the purified marine combustion oil.
2. The method of claim 1, wherein: in the step S1, the preheating temperature of the raw oil is 100-120 ℃.
3. The method of claim 1, wherein: in the step S1, the heat exchanger is located above the filter screen, and the filter screen and the heat exchanger are both inclined toward the slag discharge port of the first reaction vessel, so that the solid impurities in the feedstock oil enter the slag discharge port along the surface of the heat exchanger and the upper surface of the filter screen.
4. The method of claim 1, wherein: in step S2, the reaction tube is a spiral tube, a plurality of spiral turbulence blades are installed in the reaction tube, a plurality of heaters are installed outside the reaction tube, and the upper end of the reaction tube is communicated with the inlet end of the heat exchanger to cool the product of the glycerol esterification reaction through the heat exchanger.
5. The method of claim 1, wherein: in step S2, the molar ratio of glycerol to fatty acid in the liquid crude oil is 1:1-2:1, the temperature in the reaction tube changes in a gradient manner from 120 to 240 ℃ from bottom to top, and the glycerol and the liquid crude oil slowly flow in the reaction tube for 3 to 4 hours.
6. The method of claim 1, wherein: in the step S3, the mass of the methanol is 4-8% of that of the glycerol esterification product, KOH with the mass of the methanol being 0.5-2% of that of the glycerol esterification product is added, the reaction temperature in the second reaction kettle is 220-240 ℃, and the ester exchange time is 70-90 minutes.
7. The method of claim 1, wherein: in the step S4, pumping a product of the ester exchange reaction into a third reaction kettle, adding water with the mass of 5-10% of that of the product of the ester exchange reaction into the third reaction kettle, stirring and washing for 20 minutes at 45-55 ℃, injecting the mixture after washing into a disk centrifuge for centrifugal separation, recovering glycerol into a glycerol storage tank for recycling, and introducing the water-containing fatty acid methyl ester after centrifugation into a flash dryer for dehydration.
8. The method of claim 1, wherein: step S5, adding fatty acid methyl ester into a fourth reaction kettle, adding activated clay which accounts for 5-9% of the mass of the fatty acid methyl ester and bentonite which accounts for 5-9% of the mass of the fatty acid methyl ester into the fourth reaction kettle, stirring for 1 hour at the temperature of 80-88 ℃, and then standing for 1 hour to obtain a supernatant; adding hydrogen peroxide accounting for 3-8% of the mass of the fatty acid methyl ester into the supernatant, stirring for 30 minutes at the temperature of 80-88 ℃, standing for 1 hour, and filtering to obtain the purified marine combustion oil.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110099292.9A CN112852552A (en) | 2021-01-25 | 2021-01-25 | Method for preparing bunker fuel oil by using illegal cooking oil based on glycerol esterification process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110099292.9A CN112852552A (en) | 2021-01-25 | 2021-01-25 | Method for preparing bunker fuel oil by using illegal cooking oil based on glycerol esterification process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112852552A true CN112852552A (en) | 2021-05-28 |
Family
ID=76008756
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110099292.9A Pending CN112852552A (en) | 2021-01-25 | 2021-01-25 | Method for preparing bunker fuel oil by using illegal cooking oil based on glycerol esterification process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112852552A (en) |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106800976A (en) * | 2017-01-12 | 2017-06-06 | 中国林业科学研究院林产化学工业研究所 | A kind of method that glycerine round-robin method continous way prepares biodiesel |
-
2021
- 2021-01-25 CN CN202110099292.9A patent/CN112852552A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106800976A (en) * | 2017-01-12 | 2017-06-06 | 中国林业科学研究院林产化学工业研究所 | A kind of method that glycerine round-robin method continous way prepares biodiesel |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101029251B (en) | Biodiesel cold filtration process | |
| CN100448946C (en) | Method for conitinuously producing biological diesel oil using solid acid catalyst and piston flow reactor | |
| US20080115407A1 (en) | System and method for producing biodiesel | |
| CN100362081C (en) | Industrial producing process for coal series needle coke | |
| CN103451027B (en) | Esterification method for preparing biodiesel using waste oils and fats | |
| CN105586154A (en) | Continuous esterification method for preparing biodiesel from waste grease | |
| KR20090115248A (en) | Methanol distiller vacuum agitator combined for marking bio-diesel | |
| CN100392045C (en) | Method of synthesizing biodiesel oil using fixed bed gaseous phase esterification reaction | |
| CN101215475B (en) | Middle and low temperature preparation method for biological diesel oil by using plants fruits and seeds oil and special-purpose distillation tower for the same | |
| CN112852552A (en) | Method for preparing bunker fuel oil by using illegal cooking oil based on glycerol esterification process | |
| KR19990024530A (en) | Method and apparatus for manufacturing vegetable fuel using soybean oil or waste cooking oil | |
| US9347021B2 (en) | Process for the production of aviation biokerosene and aviation kerosene composition | |
| CN216149072U (en) | Crystallizer for refining crude biodiesel | |
| CN101343550A (en) | Production process of biological diesel oil | |
| CN100575329C (en) | Producing sebacic acid without phenol technology | |
| KR100928463B1 (en) | Method and apparatus for manufacturing single stage continuous biodiesel using pseudo multistage CRT reactor and continuous methanol recovery system | |
| CN103159590A (en) | Process for recycling excessive methyl alcohol in biodiesel production process | |
| CN103396309B (en) | A kind of method of pressurization production high-purity gallic acid propyl ester | |
| CN102154066B (en) | Method for preparing biodiesel by using xanthoceras sorbifolia oil | |
| CN111892942B (en) | Device and method for producing high-end graphite material | |
| CN101486923A (en) | Environment friendly process for biodiesel | |
| US10982159B2 (en) | Method for reducing the content of saturated monoglycerides in a raw biodiesel | |
| CN113828002B (en) | Refining method of crude biodiesel | |
| CN1029923C (en) | Method for producing coumarone resin using washing-oil residue | |
| Nugraheni et al. | Physical properties of palm oil mill effluent transesterification with local zeolite |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |