CN102206554B - Method for preparing biodiesel - Google Patents
Method for preparing biodiesel Download PDFInfo
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- CN102206554B CN102206554B CN2010101413925A CN201010141392A CN102206554B CN 102206554 B CN102206554 B CN 102206554B CN 2010101413925 A CN2010101413925 A CN 2010101413925A CN 201010141392 A CN201010141392 A CN 201010141392A CN 102206554 B CN102206554 B CN 102206554B
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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
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- 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
A method for preparing biodiesel comprises the steps of: (1) performing contact reaction between grease materials and monohydric alcohol in the presence of an acid catalyst, so that the conversion rate of fatty acid in the grease materials is higher than 80wt% and lower than 98wt%, and separating the produced water during contact reaction; (2) separating a glycerol phase and a light weight oil phase from the products obtained in the step (1); (3) in the presence of an acid catalyst, performing contact reaction between the light weight oil obtained in the step (2) and the monohydric alcohol sothat the conversion rate of the fatty acid in the light weight oil phase further becomes higher than 98wt%, and separating produced water during the contact reaction; and (4) separating biodiesel andmonohydric alcohol from the materials obtained in the step (3), recycling the obtained monohydric alcohol, and refining the obtained biodiesel to obtain the finished biodiesel product. In the method,the acid value of the grease materials is not lower than 50mg KOH/g. The yield of the biodiesel obtained by adopting the method is higher.
Description
Technical field
The present invention relates to a kind of preparation method of biofuel.
Background technology
Biofuel is a kind of long chain fatty acid ester, mainly refers to fatty acid methyl ester on the industrial application.It is to obtain by raw oil material and monohydroxy-alcohol transesterification reaction.Biofuel has the advantage of cleaning, environmental protection, compares with petrifaction diesel, and biofuel can significantly reduce carbonic acid gas, encircle the discharging of carcinogenic substances such as benzene class and pollutents such as " black smokes " more.Simultaneously, biofuel more and more receives the concern of countries in the world as reproducible raw material.
The suitability for industrialized production of biofuel depends primarily on the cost of raw oil material, and now, relatively inexpensive waste grease is the raw materials for production that people comparatively pay close attention to.Described waste grease is meant high-acid value grease, comprise the catering trade abendoned oil, as old oil (through depleted grease behind the deep fried foodstuff repeatedly), sewer oil (main source of stock oil has lard, rapeseed oil, plam oil, peanut oil and soya-bean oil etc.), acidifying oil, discarded animal oil or the like.If these waste greases can not get reasonable utilization, will bring very big problem of environmental pollution.As the raw material production biofuel, both made full use of waste grease with waste grease, reduced the pollution of waste grease, because it is cheap, can reduce the production cost of biofuel again, improved productivity effect environment.But, the characteristics of waste grease are acid number height (its acid number is generally more than 50mgKOH/g), unsaponifiable matter impurity and moisture content height, therefore, when adopting traditional catalytic ester exchange process of liquid caustic soda to prepare biofuel, must carry out acid catalysis depickling pre-treatment to waste grease earlier, make it to satisfy the catalytic ester exchange process requirement of liquid caustic soda.The catalyzer of acid catalysis depickling is the vitriol oil, and the catalytic catalyzer of liquid caustic soda is sodium hydroxide or potassium hydroxide.After carrying out the sulfuric acid catalysis depickling, free fatty acid content contained in the waste grease is reduced as much as possible, otherwise one side can increase the consumption of alkaline catalysts; On the other hand, if free fatty acid content is too high, when carrying out base catalyzed reactions, because free fatty acids and alkaline catalysts reaction have generated ester, when the washing of back, be easy to take place emulsification, perhaps make in the washing water that efflux oil phase content too high, cause the yield of biofuel to descend.Yet when carrying out the sulfuric acid catalysis depickling, when free fatty acid content takes off when being lower than 5 weight %, further the difficulty of depickling increases, and depickling time lengthening, and monohydroxy-alcohol increase as the consumption of methyl alcohol.
CN1687314A discloses a kind of technology with high acid value waste vegetable oil production biofuel, it is characterized in that: adopt the base catalysis method, under the effect of basic catalyst sodium hydroxide 1-1.2 weight %, react with methyl alcohol, by (1) removal of impurities, depickling; (2) dehydration, decolouring; (3) esterification, ester are handed over, alcoholysis; (4) four steps of phase-splitting generate fatty acid methyl ester.That is, after depickling, add alkaline catalysts production biofuel.The catalytic effect of used catalyzer is not good in this method, and the yield of the biofuel for preparing is not high.
Summary of the invention
Goal of the invention of the present invention has been to overcome among the preparation method of the biofuel that adopts prior art, after depickling, free fatty acid content is still higher, the problem that the yield of biofuel is reduced provides a kind of and can reduce the content of free lipid acid in the glyceride stock as much as possible and make the preparation method of the higher biofuel of the yield of biofuel.
The invention provides a kind of preparation method of biofuel, wherein, this method comprises the steps: that (1) is in the presence of acid catalyst, with glyceride stock and monohydroxy-alcohol contact reacts, the transformation efficiency that makes lipid acid in the glyceride stock is to being lower than 98 weight % more than the 80 weight %, described catalytic temperature is not less than the boiling temperature of described monohydroxy-alcohol and/or is not less than the boiling temperature of water, with the water that generates in catalytic separation simultaneously; (2) from step (1) products therefrom, isolate glycerine phase and lightweight oil phase; (3) in the presence of acid catalyst, lightweight oil phase and monohydroxy-alcohol contact reacts with step (2) gained, the transformation efficiency of lipid acid in the lightweight oil phase is further reached more than the 98 weight %, described catalytic temperature is not less than the boiling temperature of described monohydroxy-alcohol and/or is not less than the boiling temperature of water, with the water that generates in catalytic separation simultaneously; (4) product of step (3) gained is isolated biofuel and monohydroxy-alcohol, the monohydroxy-alcohol that obtains recycles, the biofuel that obtains after refining as product; The acid number of described glyceride stock is for being not less than 50mg KOH/g.
According to method provided by the invention, on the one hand, in reaction process, constantly separate the water that generates, break chemical equilibrium, promote that free fatty acids further reacts, to reduce the acid number of raw oil material as far as possible; On the other hand, by controlling the degree that two step transesterification reactions are carried out, fatty acid content in the raw oil material is reduced to a certain degree, promptly, the lightweight grease that generates in the separating reaction process on suitable opportunity, and, impel balance to move to the direction of positive reaction with this lightweight grease continuation and monohydroxy-alcohol reaction, impel lipid acid and unreacted glyceride stock (triglyceride level) further to be converted into biofuel, thereby the yield of the biofuel that assurance makes is higher.In addition, compared with prior art, the preparation method of biofuel provided by the invention does not adopt alkaline catalysts, eliminated the drawback that adopts alkaline catalysts to bring, for example, easily saponification reaction has taken place and cause yield to reduce, easily take place during washing to be with oil many in emulsification, the washing water, problems such as difficult treatment, increase raw material consumption, and method of the present invention is lower to the specification of quality of glyceride stock.
Embodiment
According to the present invention, the preparation method of described biofuel comprises the steps: that (1) is in the presence of acid catalyst, with glyceride stock and monohydroxy-alcohol contact reacts, the transformation efficiency that makes lipid acid in the glyceride stock is to being lower than 98 weight % more than the 80 weight %, described catalytic temperature is not less than the boiling temperature of described monohydroxy-alcohol and/or is not less than the boiling temperature of water, with the water that generates in catalytic separation simultaneously; (2) from step (1) products therefrom, isolate glycerine phase and lightweight oil phase; (3) in the presence of acid catalyst, lightweight oil phase and monohydroxy-alcohol contact reacts with step (2) gained, the transformation efficiency of lipid acid in the lightweight oil phase is further reached more than the 98 weight %, described catalytic temperature is not less than the boiling temperature of described monohydroxy-alcohol and/or is not less than the boiling temperature of water, with the water that generates in catalytic separation simultaneously; (4) product of step (3) gained is isolated biofuel and monohydroxy-alcohol, the monohydroxy-alcohol that obtains recycles, the biofuel that obtains after refining as product; The acid number of described glyceride stock is for being not less than 50mg KOH/g.
Among the present invention, the transformation efficiency of lipid acid in the described glyceride stock (or in the lightweight oil phase lipid acid) is meant that amount that lipid acid in the glyceride stock (or lightweight oil phase) and monohydroxy-alcohol reaction are converted into the lipid acid that fatty acid ester (biofuel) consumes accounts for the weight percent of total fatty acids contained in the glyceride stock, also promptly, the lipid acid that transformation efficiency (weight the %)=1-of lipid acid does not transform fully in the glyceride stock (or lightweight oil phase) accounts for the percent by weight of total fatty acids in the glyceride stock.Can be by vapor-phase chromatography measuring process (1) and step (3) thus the content of the lipid acid that does not transform fully in the products therefrom calculates the transformation efficiency of lipid acid.
In addition, the present inventor finds, in step (1), in the presence of acid catalyst, with glyceride stock and monohydroxy-alcohol contact reacts, and the transformation efficiency that makes lipid acid in the glyceride stock be more than the 80 weight % to being lower than 98 weight %, also, the acid number of glyceride stock is reduced in the scope that is higher than below 1mg KOH/g to the 20mg KOH/g; Under the preferable case, in order to be easier to control and reduce the acid number of raw oil material, and be beneficial to the yield that improves biofuel, it is 80-90 weight % that described catalytic condition makes the transformation efficiency of lipid acid in the glyceride stock, also promptly, the acid number of glyceride stock is reduced in the scope of 10mgKOH/g to 20mg KOH/g; In step (3), in the presence of acid catalyst,, the transformation efficiency of lipid acid in the lightweight oil phase is further reached more than the 98 weight % with the lightweight oil phase of step (2) gained and monohydroxy-alcohol contact reacts again, also promptly, the acid number of lightweight oil phase is reduced to below the 1mgKOH/g.That is to say, in step (1), when the acid number of glyceride stock is reduced in the scope that is higher than below 1mgKOH/g to the 20mg KOH/g, with more than the transformation efficiency of lipid acid in the glyceride stock is 80 weight % to the scope that is lower than 98 weight % be corresponding relation, and in the preferred case, when the acid number of glyceride stock is reduced in the scope of 10mg KOH/g to 20mg KOH/g, be that the scope of 80-90 weight % is corresponding relation with the transformation efficiency of lipid acid in the glyceride stock; In step (3), when the acid number of lightweight oil phase is reduced to 1mg KOH/g when following, can reach more than the 98 weight % with the transformation efficiency of lipid acid in the lightweight oil phase also is corresponding relation, therefore, in specific embodiments of the invention, promptly can corresponding learn the wherein corresponding transformation efficiency of lipid acid by the reacted glyceride stock and the greasy acid number of lightweight that provide in step (1) and the step (3).
Described acid number is meant, in and the quality (mg) of the required KOH of acidic component in the 1 gram organism.What of free acid (mainly referring to lipid acid) content in the sample are the size of acid number reflected.
According to method provided by the invention, the transformation efficiency of lipid acid reaches more than the 80 weight % to being lower than 98 weight % in the glyceride stock of controlled step (1) effectively, be preferably 80-90 weight % (promptly, the acid number of glyceride stock is reduced to be higher than below 1mg KOH/g to the 20mg KOH/g, preferably make the acid number of glyceride stock be reduced to 10mg KOH/g to 20mg KOH/g), and guarantee that described catalytic temperature is not less than the boiling temperature of described monohydroxy-alcohol and/or is not less than the boiling temperature of water, with at the catalytic water that generates that separates simultaneously; It is above (promptly to guarantee in the step (3) in the lightweight oil phase that the transformation efficiency of lipid acid further reaches 98 weight %, the acid number of lightweight oil phase is reduced to below the 1mg KOH/g), and guarantee that described catalytic temperature is not less than the boiling temperature of described monohydroxy-alcohol and/or is not less than the boiling temperature of water, with at the catalytic water that generates that separates simultaneously; Guarantee that later separation obtains the biofuel of higher yields.
In the preparation method of biofuel provided by the invention, the condition of transesterification reaction in the step (1) if in can performing step (1) in the glyceride stock transformation efficiency of lipid acid reach more than the 80 weight % to being lower than 98 weight % (that is, the acid number of glyceride stock being reduced to is higher than below the 1mg KOH/g to 20mgKOH/g).
Under the preferable case, for the transformation efficiency that guarantees lipid acid in the middle glyceride stock of step (1) reaches more than the 80 weight % to being lower than 98 weight, and preferably reach 80-90 weight %, on the one hand, control glyceride stock and the catalytic temperature of monohydroxy-alcohol, the water that gas that the gasification of under this contact reacts temperature monohydroxy-alcohol produces is generated in can be constantly with reaction system is taken out of from reactive system, to break chemical equilibrium, promotes that free fatty acids further reacts.Therefore, under the preferable case, described is 70-150 ℃ with glyceride stock and the catalytic temperature of monohydroxy-alcohol, more preferably 90-130 ℃; The mass ratio of described monohydroxy-alcohol and glyceride stock can be 0.05-2: 1, and 0.15-1.5 more preferably: 1; The consumption of described acid catalyst is the 0.1-3 weight % of glyceride stock, more preferably 0.5-2 weight %; The catalytic time can be 10 minutes-4 hours, more preferably 20 minutes-2 hours, reaches more than the 80 weight % to being lower than 98 weight with the transformation efficiency that makes lipid acid under these conditions fast, and preferably reaches 80-90 weight %.On the other hand, in order to guarantee when constantly separating moisture, guarantee to have certain reaction concentration and reaction is carried out to positive dirction in reaction mixture with the monohydroxy-alcohol of glyceride stock reaction, the described catalytic mode of monohydroxy-alcohol and glyceride stock is preferably joins monohydroxy-alcohol in the glyceride stock and monohydroxy-alcohol mixed with glyceride stock.Can select the joining day of suitable monohydroxy-alcohol according to the flow of reaction times of this step and material, for example, can adopt the step mode (adjacent twice timed interval between reinforced can be 5 seconds-2 minutes) that also can adopt of continous way that monohydroxy-alcohol is joined in the glyceride stock; Under the preferable case, in order to guarantee temperature of reaction, and the gasification of mode monohydroxy-alcohol, with monohydroxy-alcohol and glyceride stock blended mode for monohydroxy-alcohol is joined in the glyceride stock continuously.More preferably under the situation, the time of described adding monohydroxy-alcohol accounts for the 50-95% (wherein, if add monohydroxy-alcohol in the intermittent type mode, then this time that in batches adds monohydroxy-alcohol comprises adjacent twice pitch time between reinforced) of this step total reaction time.
In the step (2), the separation method that step (1) products therefrom is carried out glycerine phase and lightweight oil phase can be the separation method of the known various routines of art technology, is preferably step (1) products therefrom is carried out sedimentation or centrifugation.Described sedimentation or centrifugal condition comprise that sedimentation or centrifugal temperature are 40-90 ℃, and more preferably 45-80 ℃, sedimentation or centrifugal time are preferably 60-300 minute, more preferably 90-240 minute.
Among the preparation method of biofuel provided by the invention, the condition of the middle transesterification reaction of step (3) is as long as the transformation efficiency of lipid acid reaches 98 weight % above (that is, the acid number of lightweight oil phase being reduced to below the 1mg KOH/g) in the middle lightweight oil phase of energy performing step (3).For example, in the step (3) temperature of contact and catalyst levels can with step (1) in identical or different.Under the preferable case, in the step (3), the temperature of contact can be 70-130 ℃, more preferably 90-120 ℃; The time of contact can be 10 minutes-3 hours, more preferably 20 minutes-2 hours; The weight ratio of monohydroxy-alcohol and lightweight oil phase can be 0.05-2: 1, and 0.1-1 more preferably: 1; The consumption of described acid catalyst can be the 0.1-2 weight % of lightweight oil fat, more preferably 0.2-1 weight %.In order to guarantee when constantly separating moisture, so that reaction is carried out to positive dirction, under the preferable case, the lightweight oil phase of step (2) gained and the catalytic mode of monohydroxy-alcohol comprised monohydroxy-alcohol is joined in the lightweight oil phase, monohydroxy-alcohol is mixed with the lightweight oil phase.Can select the joining day of suitable monohydroxy-alcohol according to the flow of reaction times of this step and material, for example, can adopt the step mode (adjacent twice timed interval between reinforced can be 5 seconds-2 minutes) that also can adopt of continous way that monohydroxy-alcohol is joined in the lightweight oil phase; Under the preferable case, in order to guarantee temperature of reaction, and prevent the monohydroxy-alcohol gasification, with monohydroxy-alcohol and lightweight oil phase blended mode for monohydroxy-alcohol is joined in the lightweight oil phase continuously.More preferably under the situation, the time of described adding monohydroxy-alcohol accounts for the 50-95% (wherein, if add monohydroxy-alcohol in the intermittent type mode, then this time that in batches adds monohydroxy-alcohol comprises adjacent twice pitch time between reinforced) of this step total reaction time.
According to method provided by the invention, in the step (4), the isolating method of product of step (3) gained can be flash method, the product that is about to step (3) gained carries out flash distillation, and the temperature of flash distillation is preferably 220-260 ℃, and the time is preferably in 20 minutes.Can realize quick refining biodiesel like this, guarantee the biofuel quality.
According to method provided by the invention, wherein, under the preferable case, this method also comprises separating removes step (2) and separates the glycerine that the obtains monohydroxy-alcohol in mutually, and the monohydroxy-alcohol gas that separation obtains sent in the reaction system recycles.Described isolating method can be a flash method, and the temperature of flash distillation can be 120-160 ℃.After the flash distillation in the glycerine content of monohydroxy-alcohol be no more than 0.5 weight %, be generally 0.05-0.2 weight %.
According to method provided by the invention, the glycerine that flashes off behind the monohydroxy-alcohol gas enters refining system.Described refining system can be a mature technology well known in the art, and the present invention does not repeat them here.
Among the present invention, described grease can be various glyceride stocks, for example various animal oil and vegetables oil.When adopting method of the present invention to adopt acid number greater than 50mg KOH/g, when the waste grease that is generally 50-150mg KOH/g uses as glyceride stock, the present inventor finds, on the one hand, can remove free fatty acids and other impurity in the waste grease to greatest extent, prepare method of bio-diesel oil with existing employing waste grease and compare, the transformation efficiency of biofuel is significantly improved, on the other hand, waste grease with low cost also reduced technology cost and processing requirement.According to the present invention, described waste grease can be selected from one or more in sewer oil, acidifying oil, catering trade abendoned oil and the discarded animal oil.
Described acid catalyst can be various acid catalysts well known in the art, and for example, sulfuric acid and/or fluosulfonic acid are preferably sulfuric acid.
Described monohydroxy-alcohol can be the aliphatic monobasic alcohol of 1-4 for carbonatoms, for example can be in methyl alcohol, ethanol, propyl alcohol, Virahol and the butanols one or more, is preferably methyl alcohol.
To further describe in detail the present invention by specific embodiment below.
In the following embodiments, adopt potentiometric determination glyceride stock and the greasy acid number of lightweight.
Embodiment 1
Present embodiment is used to illustrate the preparation method of biofuel provided by the invention.
Adding 1000 gram sewer oils (acid number is 105mgKOH/g) and 20 gram mass concentration are 98% the vitriol oil in the reactor of 2 liters induction stirring, stir and heating, during to 100 ℃, 500 gram methyl alcohol are joined in the liquid in the reactor continuously, simultaneously the gas of emitting in the reactor is cooled off and collect, the process control time is 1 hour (time that adds methyl alcohol continuously is 55 minutes).Stop then stirring, material is moved out to settlement separator, 50 ℃ of following sedimentations 100 minutes, separate and remove the sub-cloud material, the upper strata material is carried out the acid number analysis, acid number is reduced to 10.5mgKOH/g.Again add upper strata material (950 gram) in the reactor, add 10 gram mass concentration and be 98% the vitriol oil, stir, be heated to 110 ℃, 300 gram methyl alcohol are joined in the reactor liquid continuously, simultaneously the gas of emitting in the reactor is cooled off and collect, the process control time is 2 hours (time that adds methyl alcohol continuously is 110 minutes), and mixture of reaction products is carried out the acid number analysis, and acid number is reduced to 1.0mgKOH/g, behind 70 ℃ thermokalite water washing upper strata material, drying is removed moisture, joins in the vacuum separator again, tells that (temperature of flash distillation is 230 ℃, time is 15 minutes) biofuel 880 gram, acid number is 0.61mgKOH/g.
Embodiment 2
Present embodiment is used to illustrate the preparation method of biofuel provided by the invention.
Adding 60 kilograms of acidifying oil (acid number is 145mgKOH/g) and 0.6 kilogram-mass concentration are 98% the vitriol oil in 100 liters stirred autoclave, stir and heating, during to 90 ℃, 60 kilograms of methyl alcohol are joined in the liquid in the reactor continuously, simultaneously the gas of emitting in the reactor is cooled off and collect, the process control time is 2.5 hours (time that adds methyl alcohol continuously is 120 minutes).Stop then stirring, material is moved out to centrifuge separator, descended centrifugal 60 minutes at 45 ℃, separate the material that removes sub-cloud, the upper strata material is carried out the acid number analysis, acid number is reduced to 11.5mgKOH/g.Again add upper strata material (53 kilograms) in the reactor, add 0.25 kilo sulfuric acid, stir, be heated to 90 ℃, 30 kilograms of methyl alcohol are joined in the reactor liquid continuously, simultaneously the gas of emitting in the reactor is cooled off and collect, the process control time is 1.5 hours (time that adds methyl alcohol continuously is 70 minutes), mixture of reaction products is carried out the acid number analysis, and acid number is reduced to 0.8mgKOH/g.Behind 70 ℃ thermokalite water washing upper strata material, drying is removed moisture, joins in the vacuum separator again, tells 49.5 kilograms of the biofuel of (temperature of flash distillation is 240 ℃, and the time is 15 minutes), and acid number is 0.53mgKOH/g.
Embodiment 3
Present embodiment is used to illustrate the preparation method of biofuel provided by the invention.
Adding 600 kilograms of discarded edible oils (acid number is 75mgKOH/g) and 9 kilogram-mass concentration are 98% the vitriol oil in the reactor of 1000 liters stirrings, stir and heating, during to 130 ℃, 900 kilograms of methyl alcohol are joined in the liquid in the reactor continuously, simultaneously the gas of emitting in the reactor is cooled off and collect, the process control time is 1.5 hours (time that adds methyl alcohol continuously is 80 minutes).Stop then stirring, material is moved out to settlement separator, 65 ℃ of following sedimentations 180 minutes, separate the material that removes sub-cloud, the upper strata material is carried out the acid number analysis, acid number is reduced to 12mgKOH/g.Again add upper strata material (540 kilograms) in the reactor, add 3 kilo sulfuric acid, stir, be heated to 120 ℃, 300 kilograms of methyl alcohol are joined in the reactor liquid continuously, simultaneously the gas of emitting in the reactor is cooled off and collect, the process control time is 0.5 hour (time that adds methyl alcohol continuously is 25 minutes), mixture of reaction products is carried out the acid number analysis, and acid number is reduced to 0.73mgKOH/g.Behind 70 ℃ thermokalite water washing upper strata material, drying is removed moisture, joins in the vacuum separator again, tells 505 kilograms of the biofuel of (temperature of flash distillation is 230 ℃, and the time is 15 minutes), and acid number is 0.66mgKOH/g.
Embodiment 4
Present embodiment is used to illustrate the preparation method of biofuel provided by the invention.
Adding discarded animal oil (acid number is 112mgKOH/g) of 550 grams and 2.75 gram mass concentration in the reactor of 1 liter induction stirring is 98% vitriol oil, stir and heating, during to 130 ℃, join 275 gram methyl alcohol in the reactor continuously, simultaneously the gas of emitting in the reactor is cooled off and collect, the process control time is 3 hours (the 110 minutes time that adds methyl alcohol).Stop then stirring, material is moved out to settlement separator, 60 ℃ of following sedimentations 150 minutes, the material that separate to remove sub-cloud is (and this lower floor's material of 150 ℃ of following flash distillations 10 minutes, and the methyl alcohol that flashes off returned again utilize, after the flash distillation in lower floor's material glycerine the content of methyl alcohol be 0.1 weight %), the upper strata material is carried out the acid number analysis, acid number is reduced to 12mgKOH/g.Again add upper strata material (510 gram) in the reactor, add 1.65 gram sulfuric acid, stir, be heated to 120 ℃, 165 gram methyl alcohol are joined in the reactor continuously, simultaneously the gas of emitting in the reactor is cooled off and collects, the process control time is 2 hours (the 75 minutes time of adding methyl alcohol), mixture of reaction products is carried out the acid number analysis, and acid number is reduced to 0.95mgKOH/g.Behind 70 ℃ thermokalite water washing upper strata material, drying is removed moisture, joins in the vacuum separator again, tells biofuel 463 grams of (temperature of flash distillation is 235 ℃, and the time is 15 minutes), and acid number is 0.7mgKOH/g.
Embodiment 5
Present embodiment is used to illustrate the preparation method of biofuel provided by the invention.
Adding discarded animal oil (acid number is 115mgKOH/g) of 550 grams and 2.75 gram mass concentration in the reactor of 1 liter induction stirring is 98% vitriol oil, stir and heating, during to 130 ℃, join 110 gram methyl alcohol in the reactor continuously, simultaneously the gas of emitting in the reactor is cooled off and collect, the process control time is 3 hours (the 120 minutes time that adds methyl alcohol).Stop then stirring, material is moved out to settlement separator, 80 ℃ of following sedimentations 240 minutes, the material that separate to remove sub-cloud is (and this lower floor's material of 150 ℃ of following flash distillations 10 minutes, and the methyl alcohol that flashes off returned again utilize, after the flash distillation in lower floor's material glycerine the content of methyl alcohol be 0.12 weight %), the upper strata material is carried out the acid number analysis, acid number is reduced to 12.5mgKOH/g.Again add upper strata material (508 gram) in the reactor, add 1.05 gram sulfuric acid, stir, be heated to 120 ℃, 400 gram methyl alcohol are joined in the reactor continuously, simultaneously the gas of emitting in the reactor is cooled off and collects, the process control time is 2 hours (the 114 minutes time of adding methyl alcohol), mixture of reaction products is carried out the acid number analysis, and acid number is reduced to 0.95mgKOH/g.Behind 70 ℃ thermokalite water washing upper strata material, drying is removed moisture, joins in the vacuum separator again, tells biofuel 460 grams of (temperature of flash distillation is 235 ℃, and the time is 15 minutes), and acid number is 0.7mgKOH/g.
Comparative Examples 1
This Comparative Examples is used to illustrate the preparation method of bio-diesel oil of prior art.
Adding 1000 gram sewer oils (acid number is 105mgKOH/g) and 150 gram mass concentration are 98% the vitriol oil in the reactor of 2 liters induction stirring, stir and heating, during to 100 ℃, 1000 gram methyl alcohol are joined in the liquid in the reactor, the reaction times is 5 hours.Stop then stirring, material is moved out to settlement separator, 50 ℃ of following sedimentations 100 minutes, separate and remove the sub-cloud material, the upper strata material is carried out the acid number analysis, acid number is reduced to 1.5mgKOH/g.Upper strata material (840 gram) is added in the reactor again, add 8.4 gram KOH alkaline catalystss, stir, be heated to 70 ℃, the process control time is 1 hour, and mixture of reaction products is carried out the acid number analysis, and acid number is reduced to 1mgKOH/g, behind 70 ℃ hot wash upper strata material, drying is removed moisture, joins in the vacuum separator again, tells that (temperature of flash distillation is 230 ℃, time is 15 minutes) biofuel 780 gram, acid number is 0.75mgKOH/g.
Claims (12)
1. the preparation method of a biofuel, it is characterized in that, this method comprises the steps: that (1) is in the presence of acid catalyst, with glyceride stock and monohydroxy-alcohol contact reacts, the transformation efficiency that makes lipid acid in the glyceride stock is to being lower than 98 weight % more than the 80 weight %, described catalytic temperature is not less than the boiling temperature of described monohydroxy-alcohol and/or is not less than the boiling temperature of water, with the water that generates in catalytic separation simultaneously; (2) from step (1) products therefrom, isolate glycerine phase and lightweight oil phase; (3) in the presence of acid catalyst, lightweight oil phase and monohydroxy-alcohol contact reacts with step (2) gained, the transformation efficiency of lipid acid in the lightweight oil phase is further reached more than the 98 weight %, described catalytic temperature is not less than the boiling temperature of described monohydroxy-alcohol and/or is not less than the boiling temperature of water, with the water that generates in catalytic separation simultaneously; (4) product of step (3) gained is isolated biofuel and monohydroxy-alcohol, the monohydroxy-alcohol that obtains recycles, the biofuel that obtains after refining as product; The acid number of described glyceride stock is for being not less than 50mg KOH/g.
2. method according to claim 1, wherein, in the step (1), the condition of reaction comprises that the mass ratio of described monohydroxy-alcohol and glyceride stock is 0.05-2:1, catalytic temperature is 70-150 ℃, the catalytic time is 10 minutes-4 hours, and the consumption of described acid catalyst is the 0.1-3 weight % of glyceride stock.
3. method according to claim 2, wherein, in the step (1), the condition of reaction comprises that the mass ratio of described monohydroxy-alcohol and glyceride stock is 0.15-1.5:1, catalytic temperature is 90-130 ℃, the catalytic time is 20 minutes-2 hours, and the consumption of described acid catalyst is the 0.5-2 weight % of glyceride stock.
4. method according to claim 1, wherein, with monohydroxy-alcohol and the catalytic mode of glyceride stock for monohydroxy-alcohol is joined in the glyceride stock; The time that adds monohydroxy-alcohol accounts for the 50-95% of this step total reaction time.
5. method according to claim 1, wherein, in the step (2), with step (1) products therefrom carry out glycerine mutually and the separation method of lightweight oil phase comprise step (1) products therefrom carried out sedimentation or centrifugation.
6. method according to claim 5, wherein, in the step (2), described sedimentation or centrifugal condition comprise that sedimentation or centrifugal temperature are 40-90 ℃, sedimentation or centrifugal time are 60-300 minute.
7. method according to claim 1, wherein, in the step (3), the condition of reaction comprises that the weight ratio of described monohydroxy-alcohol and lightweight oil phase is 0.05-2:1, catalytic temperature is 70-130 ℃, the catalytic time is 10 minutes-3 hours, and the consumption of described acid catalyst is the 0.1-2 weight % of lightweight oil phase.
8. method according to claim 7, wherein, in the step (3), the condition of reaction comprises that the weight ratio of described monohydroxy-alcohol and lightweight oil phase is 0.1-1:1, catalytic temperature is 90-120 ℃, the catalytic time is 20 minutes-2 hours, and the consumption of described acid catalyst is the 0.2-1 weight % of lightweight oil phase.
9. method according to claim 8, wherein, with the lightweight oil phase of gained and the catalytic mode of monohydroxy-alcohol for monohydroxy-alcohol is joined in the lightweight oil phase; The time that adds monohydroxy-alcohol accounts for the 50-95% of this step total reaction time.
10. method according to claim 1 wherein, in the step (4), is carried out flash distillation with the isolating method of product of step (3) gained for the product with step (3) gained, and the temperature of flash distillation is 220-260 ℃, and the time is in 20 minutes.
11. method according to claim 1, wherein, this method also comprises separating removes step (2) and separates the glycerine that the obtains monohydroxy-alcohol in mutually, and the monohydroxy-alcohol that separation obtains is recycled.
12. method according to claim 1, wherein, described monohydroxy-alcohol is that carbonatoms is the aliphatic monobasic alcohol of 1-4, and described acid catalyst is sulfuric acid and/or fluosulfonic acid, and described glyceride stock is selected from one or more in sewer oil, acidifying oil, catering trade abendoned oil and the discarded animal oil.
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| CN1746264A (en) * | 2005-09-28 | 2006-03-15 | 王建业 | Production of diesel oil from trench oil and methyl alcohol |
| CN1865401A (en) * | 2006-06-19 | 2006-11-22 | 菏泽华瑞油脂有限责任公司 | Method for preparing biological diesel oil using high acid value cottonseed oil |
| CN101531913A (en) * | 2008-03-11 | 2009-09-16 | 中国石油化工股份有限公司 | Method for preparing biodiesel |
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| CN1746264A (en) * | 2005-09-28 | 2006-03-15 | 王建业 | Production of diesel oil from trench oil and methyl alcohol |
| CN1865401A (en) * | 2006-06-19 | 2006-11-22 | 菏泽华瑞油脂有限责任公司 | Method for preparing biological diesel oil using high acid value cottonseed oil |
| CN101531913A (en) * | 2008-03-11 | 2009-09-16 | 中国石油化工股份有限公司 | Method for preparing biodiesel |
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