CN101768517A - Preparation method of biodiesel - Google Patents
Preparation method of biodiesel Download PDFInfo
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- CN101768517A CN101768517A CN201010103714A CN201010103714A CN101768517A CN 101768517 A CN101768517 A CN 101768517A CN 201010103714 A CN201010103714 A CN 201010103714A CN 201010103714 A CN201010103714 A CN 201010103714A CN 101768517 A CN101768517 A CN 101768517A
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- 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
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Abstract
The invention discloses a preparation method of biodiesel, belonging to the technical field of biodiesel preparation. In the method, volatile organic acid catalyst with the weight being 3-12% of high acid-value grease is dissolved in a certain amount of alcohol and then is mixed with the high acid-value grease, the mixture is stirred and then is heated at the temperature of 60-120 DEG C for reaction, the residual alcohol and the catalyst in the reaction liquid are removed, and the liquid at the upper layer is collected after resting and layering, so as to obtain the biodiesel. The invention has simple method, superior catalysis performance and high catalysis efficiency; in addition, the catalyst can be repeatedly recycled, and the recovery method is simple without causing the pollution of waste water.
Description
Technical field
The present invention relates to a kind of preparation method of biofuel, belong to technical field of biodiesel preparation.
Background technology
Biofuel is a fatty acid methyl ester, is a kind of renewable, environment-friendly type fuel, is typical green energy resource.In recent years, in the world particularly European and American countries government all in the development of carrying forward vigorously the biofuel industry.China is also actively developing the biofuel development.The major obstacle of present domestic restriction biofuel development is that raw materials cost is too high, uses oil crops production biofuel at home mostly, and its raw materials cost is higher, and according to statistics, 75% of the preparation cost of biofuel is a raw materials cost.Therefore, thus to adopt cheap raw material and improve that transformation efficiency reduces cost be the key that can biofuel applicable industriesization.The contour acid number oils fat raw material of sewer oil is cheap, and common high-acid value grease has plam oil, hair Rice pollard oil, Cortex jatrophae oil, waste cooking oil and oil foot etc.Utilize its preparation biofuel, can effectively reduce cost, promote the biofuel industrial expansion.
Utilize sewer oil and high acid value vegetable and animals oils to prepare biofuel at present and utilize two-step catalysis mostly, utilize acid to reduce the content of free fatty acids earlier, do biodiesel with alkali again, but process more complicated, equipment cost is high relatively a lot, and research seldom is to utilize the vitriol oil to carry out a step catalysis as catalyzer, though the feasible corrodibility to equipment of this method is bigger, requirement and input ratio to equipment are higher, and the reaction times is long.
Summary of the invention
The objective of the invention is to remedy the deficiencies in the prior art, a kind of preparation method of biofuel is provided, adopt this method a step catalysis to make biofuel, with low cost, technology is simple, and catalyst system therefor is recycling repeatedly, and can not produce contaminated wastewater.
The technical scheme that realizes the object of the invention is: a kind of preparation method of biofuel, this method is to be that the VFA catalyzer of high-acid value grease weight 3～12% is dissolved in the alcohol back and mixes with above-mentioned high-acid value grease with weight, wherein, alcohol is 15～30: 1 with the mol ratio of high-acid value grease, then under 200～500r/m agitation condition, in 60～120 ℃ of fully reactions, after having reacted, remove remaining pure and mild catalyzer in the reaction solution, standing demix is collected supernatant liquid and is obtained biofuel; Described VFA catalyzer is methanesulfonic, ethane sulfonic acid, propane sulfonic acid, butane sulfonic acid, trifluoroacetic acid, trichoroacetic acid(TCA), chlorsulfonic acid or trifluoromethanesulfonic acid.
Described high-acid value grease is the grease of acid number greater than 50mgKOH/g.
Described high-acid value grease is sewer oil, waste cooking oil, rubber seed oil, plam oil, hair Rice pollard oil, oil foot or Cortex jatrophae oil.
Described high-acid value grease is a sewer oil, and alcohol is 15～25: 1 with the mol ratio of sewer oil.
Described alcohol is methyl alcohol or ethanol.
By above technical scheme as can be known, the present invention is to be raw material with cheap high-acid value grease, utilize one step of VFA catalytic esterification, transesterification reaction to prepare biofuel, make technology obtain simplifying, reaction times shortens, and catalyst system therefor of the present invention can effectively reduce sulfuric acid and make catalyzer the time to the corrodibility of equipment, catalytic efficiency is higher than sulfuric acid catalysis, for example the activation energy of methanesulfonic catalyzed transesterification is 30.29kJ/mol, is lower than the activation energy 46.1kJ/mol of sulfuric acid catalysis.
Therefore, compared with prior art, the advantage that the present invention has is:
The inventive method is simple, and is with low cost, and the catalytic performance of catalyzer is superior, catalyzer can reclaim fully and utilize simultaneously, and recovery method is simple, rate of recovery height, and can not produce contaminated wastewater, and also solve discarded meal oil recovery simultaneously and utilized problem, have great economy, Significance for Environment.
Embodiment
In order to understand content of the present invention better, the invention will be further described below in conjunction with specific embodiment, but protection content of the present invention is not limited to following examples.
Embodiment 1
Taking by weighing 50g sewer oil (acid number 183.2mgKOH/g) pours in the there-necked flask, with weight is that the methanesulfonic of sewer oil weight 3% is dissolved in the methyl alcohol, the mol ratio of methyl alcohol and sewer oil is 20: 1, it is joined in the above-mentioned there-necked flask then, stirring velocity is 200r/m, fully reaction can react fully in general 8～15 hours under 70 ℃ of conditions, and the reaction times is 9 hours in the present embodiment.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 78.82% after measured, and the rate of recovery of catalyzer is 86.5%.
Embodiment 2
Taking by weighing 50g sewer oil (acid number 183.2mgKOH/g) pours in the there-necked flask, with weight is that the methanesulfonic of sewer oil weight 8% is dissolved in the methyl alcohol, the mol ratio of methyl alcohol and sewer oil is 15: 1, it is joined in the above-mentioned there-necked flask then, stirring velocity is 350r/m, and reaction is 10 hours under 80 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 88.82% after measured, and the rate of recovery of catalyzer is 88.5%.
Embodiment 3
Taking by weighing 50g sewer oil (acid number 183.2mgKOH/g) pours in the there-necked flask, with weight is that the methanesulfonic of sewer oil weight 12% is dissolved in the methyl alcohol, the mol ratio of methyl alcohol and sewer oil is 25: 1, it is joined in the above-mentioned there-necked flask then, stirring velocity is 400r/m, and reaction is 11 hours under 90 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 86.79% after measured, and the rate of recovery of catalyzer is 90.5%.
Embodiment 4
Taking by weighing 50 gram sewer oils (acid number 183.2mgKOH/g) pours in the there-necked flask, with weight is that the ethane sulfonic acid of sewer oil weight 10% is dissolved in the methyl alcohol, the mol ratio of methyl alcohol and sewer oil is 20: 1, it is joined in the above-mentioned there-necked flask then, stirring velocity 500r/m, reaction is 9 hours under 80 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 87.38% after measured, and the rate of recovery of catalyzer is 92.7%.
Embodiment 5
Taking by weighing 50g waste cooking oil (acid number 76.15mgKOH/g) pours in the there-necked flask, with weight is that the ethane sulfonic acid of waste cooking oil weight 12% is dissolved in the ethanol, the mol ratio of ethanol and waste cooking oil is 25: 1, it is joined in the above-mentioned there-necked flask then, stirring velocity 300r/m, reaction is 11 hours under 70 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary ethanol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 86.54% after measured, and the rate of recovery of catalyzer is 89.7%.
Embodiment 6
Taking by weighing 50g oil foot (acid number 184.9mgKOH/g) pours in the there-necked flask, with weight is that the ethane sulfonic acid of oil foot weight 3% is dissolved in the ethanol, and the mol ratio of ethanol and waste cooking oil is 15: 1, it is joined in the above-mentioned there-necked flask then, stirring velocity 350r/m, reaction is 11 hours under 70 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary ethanol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 88.32% after measured, and the rate of recovery of catalyzer is 84.5%.
Embodiment 7
Taking by weighing 50g rubber seed oil (acid number 86.15mgKOH/g) pours in the there-necked flask, with weight is that the propane sulfonic acid of rubber seed oil weight 3% is dissolved in the methyl alcohol, the mol ratio of methyl alcohol and rubber seed oil is 20: 1, join in the there-necked flask, stirring velocity 400r/m, reaction is 10 hours under 70 ℃ of conditions, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, and the upper strata is a biofuel, lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 85.23% after measured, and the rate of recovery of catalyzer is 90.7%.
Embodiment 8
Taking by weighing 50g rubber seed oil (acid number 86.15mgKOH/g) pours in the there-necked flask, with weight is that the ethane sulfonic acid of rubber seed oil weight 12% is dissolved in the methyl alcohol, the mol ratio of methyl alcohol and rubber seed oil is 25: 1, then it is joined in the there-necked flask, stirring velocity 500r/m, reaction is 10 hours under 70 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 86.50% after measured, and the rate of recovery of catalyzer is 92.1%.
Embodiment 9
Taking by weighing 50 gram plam oils (acid number 56.15mgKOH/g) pours in the there-necked flask, with weight is that the propane sulfonic acid of plam oil weight 3% is dissolved in the methyl alcohol, and methyl alcohol and palmitic mol ratio are 20: 1, then it are joined in the there-necked flask, stirring velocity 500r/m, reaction is 10 hours under 90 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 84.43% after measured, and the rate of recovery of catalyzer is 93.1%.
Embodiment 10
Taking by weighing 50 gram plam oils (acid number 56.15mgKOH/g) pours in the there-necked flask, with weight is that the butane sulfonic acid of plam oil weight 10% is dissolved in the methyl alcohol, and methyl alcohol and palmitic mol ratio are 25: 1, then it are joined in the there-necked flask, stirring velocity 450r/m, reaction is 10 hours under 90 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 85.89% after measured, and the rate of recovery of catalyzer is 90.8%.
Embodiment 11
Taking by weighing 50 gram plam oils (acid number 56.15mgKOH/g) pours in the there-necked flask, with weight is that the butane sulfonic acid of plam oil weight 12% is dissolved in the methyl alcohol, and methyl alcohol and palmitic mol ratio are 25: 1, then it are joined in the there-necked flask, stirring velocity 400r/m, reaction is 10 hours under 90 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 85.89% after measured, and the rate of recovery of catalyzer is 90.8%.
Embodiment 12
Taking by weighing 50g hair Rice pollard oil (acid number 63.8mgKOH/g) pours in the there-necked flask, the chlorsulfonic acid of weight for hair Rice pollard oil weight 3% is dissolved in the methyl alcohol, methyl alcohol is 25: 1 with the mol ratio of hair Rice pollard oil, then it is joined in the there-necked flask, stirring velocity is 300r/m, and reaction is 8 hours under 90 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 89.78% after measured, and the rate of recovery of catalyzer is 93.4%.
Embodiment 11
Taking by weighing 50g hair Rice pollard oil (acid number 63.8mgKOH/g) pours in the there-necked flask, the chlorsulfonic acid of weight for hair Rice pollard oil weight 12% is dissolved in the methyl alcohol, methyl alcohol is 20: 1 with the mol ratio of hair Rice pollard oil, then it is joined in the there-necked flask, stirring velocity is 250r/m, and reaction is 15 hours under 90 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 84.53% after measured, and the rate of recovery of catalyzer is 86.4%.
Embodiment 12
Taking by weighing 50g hair Rice pollard oil (acid number 63.8mgKOH/g) pours in the there-necked flask, the chlorsulfonic acid of weight for hair Rice pollard oil weight 8% is dissolved in the methyl alcohol, methyl alcohol is 20: 1 with the mol ratio of hair Rice pollard oil, then it is joined in the there-necked flask, stirring velocity is 500r/m, and reaction is 12 hours under 90 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 88.22% after measured, and the rate of recovery of catalyzer is 91.4%.
Embodiment 13
Taking by weighing 50g hair Rice pollard oil (acid number 63.8mgKOH/g) pours in the there-necked flask, the trichoroacetic acid(TCA) of weight for hair Rice pollard oil weight 8% is dissolved in the methyl alcohol, methyl alcohol is 20: 1 with the mol ratio of hair Rice pollard oil, then it is joined in the there-necked flask, stirring velocity is 300r/m, and reaction is 9 hours under 60 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 86.32% after measured, and the rate of recovery of catalyzer is 90.5%.
Embodiment 14
Taking by weighing 50g hair Rice pollard oil (acid number 63.8mgKOH/g) pours in the there-necked flask, the trichoroacetic acid(TCA) of weight for hair Rice pollard oil weight 8% is dissolved in the methyl alcohol, methyl alcohol is 25: 1 with the mol ratio of hair Rice pollard oil, then it is joined in the there-necked flask, stirring velocity is 500r/m, and reaction is 9 hours under 80 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 87.02% after measured, and the rate of recovery of catalyzer is 87.5%.
Embodiment 15
Taking by weighing 50g hair Rice pollard oil (acid number 63.8mgKOH/g) pours in the there-necked flask, the trichoroacetic acid(TCA) of weight for hair Rice pollard oil weight 8% is dissolved in the methyl alcohol, methyl alcohol is 25: 1 with the mol ratio of hair Rice pollard oil, then it is joined in the there-necked flask, stirring velocity is 450r/m, and reaction is 15 hours under 90 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 88.25% after measured, and the rate of recovery of catalyzer is 89.5%.
Embodiment 16
Taking by weighing 50g Cortex jatrophae oil (acid number 73.5mgKOH/g) pours in the there-necked flask, with weight is that the trifluoroacetic acid of Cortex jatrophae weight of oil 3% is dissolved in the methyl alcohol, the mol ratio of methyl alcohol and Cortex jatrophae oil is 30: 1, then it is joined in the there-necked flask, stirring velocity is 300r/m, and reaction is 8 hours under 120 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 86.07% after measured, and the rate of recovery of catalyzer is 93.1%.
Embodiment 17
Taking by weighing 50g Cortex jatrophae oil (acid number 73.5mgKOH/g) pours in the there-necked flask, with weight is that the trifluoroacetic acid of Cortex jatrophae weight of oil 8% is dissolved in the methyl alcohol, the mol ratio of methyl alcohol and Cortex jatrophae oil is 25: 1, then it is joined in the there-necked flask, stirring velocity is 400r/m, and reaction is 10 hours under 100 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 88.28% after measured, and the rate of recovery of catalyzer is 90.5%.
Embodiment 18
Taking by weighing 50g Cortex jatrophae oil (acid number 73.5mgKOH/g) pours in the there-necked flask, with weight is that the trifluoroacetic acid of Cortex jatrophae weight of oil 12% is dissolved in the methyl alcohol, and the mol ratio of methyl alcohol and Cortex jatrophae oil is 20: 1, joins in the there-necked flask, stirring velocity is 500r/m, and reaction is 12 hours under 90 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, lower floor is a glycerine, upper strata liquid is collected air inlet detect esterification yield mutually, and lower floor's liquid rotary evaporation reclaims catalyzer, esterification yield is 87.32% after measured, and the rate of recovery of catalyzer is 93.1%.
Embodiment 19
Taking by weighing 50g Cortex jatrophae oil (acid number 73.5mgKOH/g) pours in the there-necked flask, with weight is that the trifluoromethanesulfonic acid of Cortex jatrophae weight of oil 3% is dissolved in the methyl alcohol, the mol ratio of methyl alcohol and Cortex jatrophae oil is 20: 1, then it is joined in the there-necked flask, stirring velocity is 500r/m, and reaction is 8 hours under 90 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 88.02% after measured, and the rate of recovery of catalyzer is 95.1%.
Embodiment 20
Taking by weighing 50g Cortex jatrophae oil (acid number 73.5mgKOH/g) pours in the there-necked flask, with weight is that the trifluoromethanesulfonic acid of Cortex jatrophae weight of oil 7% is dissolved in the methyl alcohol, the mol ratio of methyl alcohol and Cortex jatrophae oil is 25: 1, then it is joined in the there-necked flask, stirring velocity is 400r/m, and reaction is 13 hours under 90 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, adopts vapor-phase chromatography to detect esterification yield, and esterification yield is 92.78% after measured, and the rate of recovery of catalyzer is 93.8%.
Embodiment 21
Taking by weighing 50g Cortex jatrophae oil (acid number 73.5mgKOH/g) pours in the there-necked flask, with weight is that the trifluoromethanesulfonic acid of Cortex jatrophae weight of oil 12% is dissolved in the methyl alcohol, the mol ratio of methyl alcohol and Cortex jatrophae oil is 30: 1, then it is joined in the there-necked flask, stirring velocity is 500r/m, and reaction is 12 hours under 90 ℃ of conditions.After reaction finishes, take out the reaction solution rotary evaporation and remove unnecessary methyl alcohol, and pour standing demix in the separating funnel into, the upper strata is a biofuel, and lower floor is a glycerine; Upper strata liquid is collected air inlet detect esterification yield mutually, lower floor's liquid rotary evaporation reclaims catalyzer, and esterification yield is 94.23% after measured, and the rate of recovery of catalyzer is 93.1%.
Claims (5)
1. the preparation method of a biofuel, it is characterized in that: with weight is that the VFA catalyzer of high-acid value grease weight 3～12% is dissolved in the alcohol back and mixes with above-mentioned high-acid value grease, wherein, alcohol is 15～30: 1 with the mol ratio of high-acid value grease, then under 200～500r/m agitation condition, in 60～120 ℃ of fully reactions, after having reacted, remove remaining pure and mild catalyzer in the reaction solution, standing demix is collected supernatant liquid and is obtained biofuel; Described VFA catalyzer is methanesulfonic, ethane sulfonic acid, propane sulfonic acid, butane sulfonic acid, trifluoroacetic acid, trichoroacetic acid(TCA), chlorsulfonic acid or trifluoromethanesulfonic acid.
2. the preparation method of biofuel according to claim 1, it is characterized in that: described high-acid value grease is the grease of acid number greater than 50mgKOH/g.
3. the preparation method of biofuel according to claim 2 is characterized in that: described high-acid value grease is sewer oil, waste cooking oil, rubber seed oil, plam oil, hair Rice pollard oil, oil foot or Cortex jatrophae oil.
4. the preparation method of biofuel according to claim 1, it is characterized in that: described high-acid value grease is a sewer oil, alcohol is 15～25: 1 with the mol ratio of sewer oil.
5. according to the preparation method of claim 1 or 4 described biofuel, it is characterized in that: described alcohol is methyl alcohol or ethanol.
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| CN201010103714A CN101768517A (en) | 2010-01-28 | 2010-01-28 | Preparation method of biodiesel |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102154064A (en) * | 2011-03-11 | 2011-08-17 | 江苏恒顺达生物能源有限公司 | Preparation method of biodiesel |
| CN102553643A (en) * | 2012-01-18 | 2012-07-11 | 山东锦江生物能源科技有限公司 | Composite catalyst for producing biodiesel and production method for composite catalyst |
| CN103468413A (en) * | 2013-09-25 | 2013-12-25 | 陕西合盛生物柴油技术开发有限公司 | Production method of biodiesel |
| CN106753814A (en) * | 2017-03-03 | 2017-05-31 | 云南盈鼎生物能源股份有限公司 | A kind of low-sulfur, the production method without sulphur, high ester content biodiesel |
-
2010
- 2010-01-28 CN CN201010103714A patent/CN101768517A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102154064A (en) * | 2011-03-11 | 2011-08-17 | 江苏恒顺达生物能源有限公司 | Preparation method of biodiesel |
| CN102553643A (en) * | 2012-01-18 | 2012-07-11 | 山东锦江生物能源科技有限公司 | Composite catalyst for producing biodiesel and production method for composite catalyst |
| CN102553643B (en) * | 2012-01-18 | 2013-07-31 | 山东锦江生物能源科技有限公司 | Composite catalyst for producing biodiesel and production method for composite catalyst |
| CN103468413A (en) * | 2013-09-25 | 2013-12-25 | 陕西合盛生物柴油技术开发有限公司 | Production method of biodiesel |
| CN103468413B (en) * | 2013-09-25 | 2014-08-27 | 陕西合盛生物柴油技术开发有限公司 | Production method of biodiesel |
| CN106753814A (en) * | 2017-03-03 | 2017-05-31 | 云南盈鼎生物能源股份有限公司 | A kind of low-sulfur, the production method without sulphur, high ester content biodiesel |
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Application publication date: 20100707 |