CN104136581A - Production of biofuel from tobacco plants - Google Patents

Production of biofuel from tobacco plants Download PDF

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Publication number
CN104136581A
CN104136581A CN201280065904.1A CN201280065904A CN104136581A CN 104136581 A CN104136581 A CN 104136581A CN 201280065904 A CN201280065904 A CN 201280065904A CN 104136581 A CN104136581 A CN 104136581A
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China
Prior art keywords
tobacco
biofuel
biomass
organic solvent
oil
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CN201280065904.1A
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Chinese (zh)
Inventor
罗纳德·T·佩鲁索
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Delaware Paddy Agricultural Sciences Institute
Delaware Valley College of Science and Agriculture
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Delaware Paddy Agricultural Sciences Institute
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    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • 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
    • C10L1/026—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only for compression ignition
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B1/00—Production of fats or fatty oils from raw materials
    • C11B1/10—Production of fats or fatty oils from raw materials by extracting
    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C67/00—Preparation of carboxylic acid esters
    • C07C67/02—Preparation of carboxylic acid esters by interreacting ester groups, i.e. transesterification
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C10G2300/1014—Biomass of vegetal origin
    • 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
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Abstract

A method of producing biofuel from tobacco biomass including solvent extraction of the tobacco biomass with methyl acetate or ethyl acetate, transesterification of the oil obtained from the biomass and separation of the biofuel from the transesterified product. Excellent yields of biofuel based on the weight of the biomass are obtained.

Description

By tobacco plant, produced the method for biofuel
Background of invention
Description of Related Art
The mankind have the history of very long plantation tobacco, and first it be as ornamental plant and medicinal plant, then as luxury goods.In the most of the time of modern historical, the mankind to the use of tobacco based on leaf being converted into smoking, inhalation of dust and chewing article.Recently, other purposes of tobacco has been proposed, as for producing food proteins (alimentaryprotein) by leaf by purification, for the pharmacology effective active composition that is conventionally present in leaf is provided, and as the source of the recombinant protein of expressing in the leaves of transgenic plant or seed.Another promising purposes of tobacco is as the fuel source that produces green energy resource.
Use the negative consequences of fossil oil on environment and limited operability thereof for the research of new forms of energy provides motivation.In these new forms of energy, biofuel is because its recyclability is a possible selection.The biofuel in agricultural source is mainly the bio-ethanol for example, for example, being made by the plant that produces monose (sucrose) or complex sugar (Mierocrystalline cellulose).Model plant for this production has been defined as sugarcane, corn, wheat, potato, cassava, beet, barley, Chinese sorghum etc.As selection, prior art has developed into by produce oil or non-produce oil but has been rich in oily kind produces oil fuel and biofuel as soybean, Sunflower Receptacle, rape, peanut, flax, corn, sesame, palm, palm-kernel, coconut, castor-oil plant etc.
Biofuel is the energy as an alternative, with respect to bio-ethanol, has some advantages.One of them advantage Shi U.S. is corn and the soybean as staple food crop for obtaining the main raw material of bio-ethanol.In addition, bio-ethanol production is conventionally poor than the efficiency of production of biodiesel.For example, the energy of the energy many 25% that corn ethanol drops in only producing and producing than it, and biofuel can produce than needing the energy dropping into have more the energy up to 93% in its production.Finally, bio-ethanol produces more greenhouse gases than biofuel.With respect to fossil oil, produce and the greenhouse gas emission of burning bio-ethanol reduces nearly 12%, produce and use biofuel to reduce nearly 41%.The every net energy gain of biofuel (net energy gain) also discharges air pollutant (Hill et al. still less than bio-ethanol, Environmental, economic, and energetic costs and benefitsof biodiesel and ethanol biofuels (environment of biofuel and alcohol biological fuel, economy and energy cost and income), Proc Natl Acad Sci USA.2006,103 (30): 11206-11210).
Biofuel from tobacco can be an important supplement to the renewable energy source strategy of our country.Current trend concentrates on and from tobacco seed, extracts oil.According to estimating in world wide, surpass the tobacco production of 4,000,000 hectares, tobacco seed can be feasible substitute energy.Yet tobacco biomass, particularly leaf are left in the basket in fact and produce for biofuel.Tobacco plant can produce the low cost of about 170 tons/acre, the biological material of high value, and there is no high labour demand, chemical input or geographic restrictions.Tobacco plant has very large leaf area, little inflorescence and the highest over-ground part of observing in agricultural plants and the ratio of root.Similar with palohierror, after being cut down, tobacco will be from its stump germinating (coppice) or rudiment again.Germinating makes several times a year to gather in the crops and becomes possibility, and this makes it can produce very high biomass tonnage (biomasstonnage).In addition, tobacco can grow up strong and sturdy on different types of soil in extensive environment.Finally, because tobacco is the non-food crop that can grow up strong and sturdy in lean soil, so it can not fight for more fertile soil as corn and soybean with food crop.
US2010/0184130 discloses engineered tobacco plant and has extracted oily method by its biomass.Genetically engineered can increase the oleaginousness (oil deposits) in tobacco leaf.The method is used improved hexane extraction method from biomass, to obtain oil.
US2009/0234146 discloses from biomass as the method for extraction and ester-exchanged oil plant or algae.This extracting method comprises with the cosolvent system that comprises at least one polar covalence molecule and at least one ionic liquid processes biomass.This polar covalence molecule can be methyl acetate.With methyl alcohol, using sodium hydroxide as catalyzer or using sulfuric acid with methyl alcohol and as catalyzer, complete the oily transesterify of extraction.Yet the document is not mentioned tobacco.
The object of the invention is to increase to be extracted oil and processes oily efficiency from tobacco biomass, thereby it will be suitable for use as biofuel.
Invention field
The present invention relates to extract from plant biomass the method for lipid or oil.Particularly, the present invention relates to be obtained by tobacco plant the method for biofuel.
Summary of the invention
The method that the present invention relates to be produced by tobacco biomass biofuel, comprises the following steps: with polar organic solvent, extract tobacco biomass, the oil of separation and Extraction from polar organic solvent, the oil that transesterify is extracted separating bio fuel from reaction mixture.
Detailed description of preferred embodiments
For purposes of illustration, by principle of the present invention being described with reference to various exemplary.Although specifically described certain embodiments of the present invention herein, those of ordinary skill in the art will easily recognize, same principle is equally applicable to and can be used in other system and method.Before in detail explaining disclosed embodiments of the present invention, should understand the present invention and not limit it and be applied to the details in any specific embodiments illustrating.In addition the object that, term used herein is used to describe rather than limit.And although some method is to describe with reference to the step occurring by a certain order herein, in many cases, these steps can be carried out according to the intelligible any order of those skilled in the art; Therefore this novel method is not limited to the step of ad hoc arrangement disclosed herein.
Should be noted that, unless the context clearly indicates, herein with appended claim in the singulative " (a) ", " one (an) " that use and " should (the) " comprise a plurality of indicators (plural references).And term " (a) " (or " (an) "), " one or more (one or more) " and " at least one (at least one) " can exchange use in this article.Term " comprises (comprising) ", " comprising (including) ", " having (having) " and " by ... (the constructed from) of formation " also can be exchanged use.
Aspect first, the present invention relates to by biomass, particularly by tobacco, produced the method for biofuel.In this respect, first use polar organic solvent from biomass, to extract the oil in tobacco biomass.Then oil is carried out to transesterify, generate the lipid acid that is suitable for use as biofuel.
Term used herein " biomass (biomass) " refers in fact the derivative organic substance of any tobacco plant.It comprises in complete plant, plant organ (being leaf, stem, flower, root etc.), seed, vegetable cell (comprising tissue culture cells), aforementioned project one or more offspring and the pulverised form of this material.
The tobacco plant of any kind and type can be for the present invention.The tobacco in its biomass with high oil or lipid content is the preferred tobacco type for the present invention.For example, nanowatt Huoshan tobacco (Navajo Mountain tobacco), has relatively high oil-contg in its biomass, is the preferred tobacco type for the present invention.Can also use and through genetically engineered, make in its biomass, to there is high oil or the tobacco plant of lipid content.Applicable rotaring gene tobacco plant comprises those that describe in following document, Andrianov et al. for example, " Tobacco as a production platformfor biofuel:overexpression of Arabidopsis DGAT and LEC2genes increasesaccumulation and shifts the composition of lipids in green biomass (as the tobacco of biofuel production platform: the crossing to express to have increased the accumulation of lipid in green bio matter and changed it of Arabidopis thaliana DGAT and LEC2 gene forms) ", Plant Biotechnol J., Vol.8, pages277-87 (2009), and US2010/0184130.
In some embodiments of the present invention, may wish that water planting plantation tobacco plant, to realize rapid growth, obtains higher yields and/or carries out plant growing the whole year.Water planting plantation allows to plant tobacco plant under highly controlled, reproducible condition, is convenient to effectively gather in the crops a large amount of thread root systems with clean, complete state.
For tabacco water, cultivate the illustrative methods of planting as follows.Make tobacco seed on the surface of moist green plant mixture (plant potting mixture) or near germination.Applicable condition is the temperature of approximately 80 ℉ and 60% relative humidity.After seed germination approximately two weeks, prune (removing) seedling and grow to it and have an appointment 6 inches high and there is stage of approximately 6 leaves for remaining seedling is without hindrance to reserve enough spaces.When seedling reaches approximately 6 inches high, conventionally it is migrated to the hydroponic device that contains applicable nutritive medium and install for the ventilation (oxidation) of nutritive medium together with complete root system and pot material particle.The nutrient substance that this hydroponic device is also tackled dissolving provides supplementary, and should have enough sizes to hold full-grown tobacco plant.
Can also use other applicable implantation methods.For example, can plant tobacco in as the soil of coconut fiber thering is extraneous growth matrix.Although can preferably plant tobacco for scale operation in greenhouse, conventionally can adopt the outdoor plantation being applicable in weather.
When growth is complete, by tobacco plant results, and from biomass, extract oil and/or lipid.The various piece of tobacco plant, comprises that stem, root, leaf and/or seed can be for extraction steps of the present invention.Those skilled in the art also will understand, and the condition of extraction process can be adjusted as required, so that it is optimized for one or more biomass of using.
Can before extraction step, to tobacco biomass, carry out pre-treatment.This pre-treatment step can include but not limited to one or more in the following step: separating biomass from growth matrix, dry these biomass and physics or these biomass of mechanical disintegration are to increase its surface-area.Can use any method well known by persons skilled in the art to carry out this pre-treatment step.For example, can be by centrifuging separating biomass from growth matrix, with deionized water rinsing further to remove micro-growth matrix, vacuum-drying or lyophilize.
Can be by tobacco biomass is contacted to form extraction mixture with polar organic solvent, thereby being extracted to enter, the oil of biomass and/or lipid composition in solvent, carry out extraction step.Once complete required extracted amount, from extracting the remaining biomass of mixture separation.
This polar organic solvent can be selected from methyl acetate and ethyl acetate.
This leaching process can be used the organic solvent of any suitable amount.For example, every gram of biomass can be used the organic solvent of 1-4 gram of amount.Biomass and polar organic solvent are unimportant in conjunction with the mode of extracting mixture with formation, therefore biomass can be joined in polar organic solvent or polar organic solvent can be joined in biomass.
Form to extract after mixture, can in envrionment temperature, for example keep time enough to extract most oil or lipid from tobacco biomass at 15-25 ℃ it.Alternatively, can will extract mixture stirring heating to as high as the temperature of extracting the boiling point of minimum boiling point polar organic solvent in mixture.Extraction time can be between approximately 1 hour to approximately 48 hours, and it depends on type and amount, the type of solvent and the step of whether carrying out other method as heated or being convenient to extract of biomass.Those skilled in the art can determine optimum extraction time by simple experiment.Preferably, at the temperature of approximately 60 ℃ to approximately 65 ℃, carry out the extraction of approximately 16 hours to approximately 48 hours.
In some embodiments, can process by using ultrasound, stir, pressurization and/or quantity of radiant energy (for example microwave, infrared rays) strengthen the extraction of polar organic solvent to tobacco biomass, thereby increase extraction rate and efficiency.
After extracting and substantially completing, as determined as the case may be, the main economy based on extraction process, can be to extracting that mixture carries out extra step so that from extract mixture the oil of separation and Extraction.For example, can use centrifuging or filtration method to remove remaining biomass from extract mixture.Can also from extraction, remove polar organic solvent mixture by for example rotary evaporation or distillation as vacuum distilling.
It is unsatisfactory that the oil extracting from tobacco biomass is directly used in combustion engine.Therefore, by the oil of extraction and low-molecular-weight alcohol being carried out to transesterify as methyl alcohol or ethanol react to oil under the existence of catalyzer.This transesterification reaction comprises the exchange of ester group, and therefore generates two products: fatty acid ester (as the useful component of biofuel) and glycerine (conventionally being sold for the valuable by product in soap and other products).Another by product of reaction is a kind of natural sterilant source, and it can be separated and sells separately as the another kind of product of this technique.Before carrying out step of transesterification, caustic compounds and water can be joined in tobacco oil, thereby carry out routine " soda finishing (alkali refining) " step.
Thereby can by under the existence of catalyzer by oil and low-molecular-weight alcohol as methanol mixed formation reaction mixture, carry out Exchange Ester Process.Transesterify can be acid catalyzed transesterify or the step of transesterification of base catalysis.The catalyzer using in step of transesterification can be an acidic catalyst or basic catalyst.Acid catalyst can be protonic acid (Bronsted acid), and it is that sulfonic acid or sulfuric acid type are sour, H 2sO 4, HC1, Acetyl Chloride 98Min., BF 3deng.Alkaline catalysts can be for example KOH, NaOH, NaOCH 3, Na 2cH 2cH 3, guanidine (for example 1,5,7-tri-azabicyclos [4.4.0] last of the ten Heavenly stems-5-alkene (TBD)); And M (3-hydroxy-2-methyl-pyrokomane) 2 (H 2)) 2the metal complex of type, wherein M=Sn, Zn, Pb or Hg.Can also use K 2cO 3, the solvable KOCH of its methanol 3and the insoluble KHCO of ethanol 3.In an exemplary, with 6% amount of oil mass, use K 2cO 3for Exchange Ester Process.
The transesterification reaction conventionally temperature below alcohol boiling point (general approximately 65 ℃) is carried out at least 30 minutes.Due to alcohol and oil component limited mutual solubility only each other, this bi-phasic reaction mixture of vigorous stirring and/or can use phase-transfer catalyst to accelerate transesterification reaction.Conventionally, the transesterify time that acid catalyst need to be longer than alkaline catalysts.In preferred embodiments, with respect to using alkaline catalysts, acid catalyst in transesterification reaction mixture with more substantial alcohol coupling.
The alcohol that is suitable for being used in Exchange Ester Process can be any low-molecular-weight alcohol preferably with no more than four carbon atom, as methyl alcohol or ethanol.Conventionally in reaction mixture, use the alcohol excessive with respect to oily amount, with driving a reaction, be conducive to the production of fatty acid ester.In reaction mixture, alcohol should be at least about 3:1 with mol ratio that can ester-exchanged oil, at the most 6:1.This ratio can change according to the alkali using.
When transesterification reaction mixture reaches the point that approaches balance, while being conventionally approximately 80% with respect to the glyceryl ester transformation efficiency of total fatty acids ester in reaction mixture, can allow reaction mixture to precipitate about 12-24 hour.Thereafter, separable nonpolar phase, and with new alcohol and the catalyzer mixing, repeat this reaction alternatively.After optional the second step of transesterification is carried out, by upper strata nonpolar phase (biofuel phase) separation, and evaporate alternatively or distill with from wherein removing alcohol.
If desired, conventional oil additive can be joined in the biofuel obtaining as improved the additive of cold resistance, burning, stability in storage etc.
Can process by using ultrasound, micro-heating, stirring, pressurization and/or quantity of radiant energy (for example microwave, infrared rays) strengthen transesterify.For example, can follow stirring that multi-phase reaction mixture is heated to the temperature below alcohol boiling point.
Directly the time length of transesterification reaction can be approximately 1 hour to approximately 48 hours or more of a specified duration, until substantially complete direct transesterification reaction.Substantially the reaction completing preferably can not obtain the amount of product or the reaction that concentration further increases significantly by further reaction under the reaction conditions using.After directly transesterification reaction completes substantially, can carry out extra processing so that reaction product is further separated each other to multi-phase reaction mixture.For example, multi-phase reaction mixture can be carried out to centrifugation, and can or move liquid and enter independent container and take out the composition that comprises fatty acid ester product by for example decant (decanting).
In some embodiments, can be by with solvent after transesterify, if non-polar solvent is as hexane, or the mixture of the mol ratio Virahol that is 5:4 and hexane extracts the product of the fatty acid esters of purifying.Can add some alkali if sodium hydroxide is to promote this separation.If use this solvent extraction, subsequently can be by for example carrying out separated product from solvent from product evaporating solvent under vacuum.
Alternatively, can wash the product of fatty acid esters with water.In one embodiment, this product mixes with the distilled water of isodose, keeps standing 24 hours, and separated from water.Can use anhydrous sodium sulphate or another kind of applicable water-absorbing material from the product of fatty acid esters, to absorb any remaining water.
Alternatively, polar organic solvent recovery and recirculation can be used for to another direct transesterification reaction or leaching process.Can by for example by reaction mixture centrifugation so that the biomass balling-up of processing decant solvent and rotary evaporation carry out solvent recuperation.Can also be by wherein reclaiming polar organic solvent with the mechanical filter of the gradual a series of mesh gauze filters that successively decrease of hole.
The catalyzer using in step of transesterification can be an acidic catalyst or basic catalyst.This acid catalyst can be protonic acid.This acid catalyst can be selected from sulfonic acid or sulfuric acid as H 2sO 4, HC1, Acetyl Chloride 98Min., BF 3deng.Alkaline catalysts can be for example KOH, NaOH, NaOCH 3, Na 2cH 2cH 3, guanidine (for example 1,5,7-tri-azabicyclos [4.4.0] last of the ten Heavenly stems-5-alkene (TBD)); And M (3-hydroxy-2-methyl-pyrokomane) 2 (H 2)) 2the metal complex of type, wherein M=Sn, Zn, Pb or Hg.
In one exemplary embodiment, Acetyl Chloride 98Min. can be as the catalyzer in the transesterification reaction of use methyl alcohol.Catalytic effect is two-step reaction, and wherein first Acetyl Chloride 98Min. reacts with methyl alcohol and form methyl acetate and be dissolved in the gaseous hydrogen chloride in methyl alcohol.Then hydrogenchloride is protonated by the ketonic oxygen of glyceryl ester, promotes the exchange of ester group in glyceryl ester.
The selection of concrete tobacco type, growth conditions be concrete setting, the concrete selection of extracting solvent and the use of transesterification reaction of water planting plantation for example, and in these factors, one or more combination produces the biofuel with respect to total plant quality higher yields.Particularly, use the nanowatt Huoshan tobacco growing under water planting condition, by methyl acetate or ethyl acetate, extracting and carry out transesterification reaction provides the biofuel with respect to the special high yield of total plant quality.
Biofuel product contains the fatty acid ester of high per-cent conventionally, and they are desirable fuel products.The key existing in fatty acid ester can be measured by infrared analysis.The methyl alcohol existing in the hydrocarbon chain of biological example fuel and two key (trans or cis) can be determined in this way.Equally, can identify in this way SP2 carbon atom.Infrared analysis can also be for determining the composition of product methyl esters.
Thin-layer chromatography (TLC) can be for measuring the amount of unreacted triglyceride level in composition.For the solvent of TLX, can be for example 85ml hexane, 15ml ether and 1ml HC 2h 3o 2mixture.
Viscometry (Viscometry) can be for measuring relative viscosity.This can be by comparing product viscosity and control group oil to realize.
The combustionproperty of biofuel can be for example by being used bomb calorimeter (BombCalorimeter) to measure.
Provide following non-limiting example to further illustrate embodiment of the present invention.It will be appreciated by those skilled in the art that in following examples, disclosed technology represents the method for implementing well in practice of the present invention that inventor finds, and therefore can be considered to form the example for its practice model.Yet those skilled in the art, according to content disclosed by the invention, should understand in the situation that not departing from the scope of the invention, in disclosed specific embodiments, can make many changes and still can obtain same or similar result.
Embodiment 1-extracts
Dry tobacco leaf (9.2000g) before oil extracts.Use the commercial shredder of 19000rpm to grind leaf.The slurry obtaining is placed in to the porcelain sleeve (thimble) of methyl acetate.Solvent deepens in time, until observe middle deep green after approximately three hours.Use afterwards apparatus,Soxhlet's (Soxhlet extractor) to extract 2 hours.In round-bottomed flask, with solvent, tobacco oil is reclaimed.Distillation is except desolventizing afterwards.Use sodium sulfate to remove any moisture in tobacco oil.Obtain 5.00ml oil.As a comparison case, use rotatory evaporator for removing desolventizing, and extraction solvent is methyl acetate and hexane.
Embodiment 2-transesterify
Using 3.028g tobacco oil and 1%H as the 10ml of catalyzer 2sO 4, 10ml methyl alcohol and 40ml Virahol (70%)/hexane the mixture of 5:4 mix.In a version, by CH 3oH/ oil and 5%H 2sO 4press the mixed in molar ratio of 40:1.Use the bottom of separated pH～7.5 of separating funnel.By this bottom micro-filtration, then add Na 2sO 4, subsequently that it is separated from the biofuel product generating.
Embodiment 3-product characterizes
By the oil samples of the titration mixing with 70%2-propyl alcohol, measure the acid number of biofuel product.Use the standard titration process of 0.1M KOH.
In addition by the glycerine in iodimetric titration (Iodiometric titration) detection of biological diesel product.Glycerine in biofuel is reduced to iodate by periodate.Iodate or any remaining periodate are measured with reacting of thiosulphate by it.The reducing amount of thiosulphate after reaction is compared with control group, wherein the periodate of identical initial amount and thiosulfuric acid reactant salt.Result has shown the amount of the glycerine that exists in biofuel.Total glycerine in biofuel of the present invention is measured as the 0.25wt% that is less than biofuel, and free glycerol is less than the 0.02wt% of biofuel.
Yet, what know is, although mentioned the detailed description of many feature and advantage of the present invention and structure and function of the present invention in above stated specification, but above stated specification is only illustrative, and can make a change in detail, particularly in concept of the present invention, the layout key element to shape, size and each several part makes a change, change at utmost as widely as shown in general sense of appending claims term used.

Claims (18)

1. by tobacco biomass, produced a method for biofuel, comprise the following steps:
With the polar organic solvent that is selected from methyl acetate and ethyl acetate, from described tobacco biomass, extract oil,
Remove described polar organic solvent,
The oil that transesterify is extracted, and
Separated described biofuel from the product of step of transesterification.
2. the method for claim 1, further comprising the steps of:
Before contacting with polar organic solvent, pulverize described tobacco biomass.
3. the method for claim 1, wherein said organic solvent is methyl acetate.
4. the method for claim 1, the amount of wherein said polar organic solvent is every gram of about 1-4 gram of biomass.
5. the method for claim 1, wherein said extraction is carried out approximately 16 hours to 48 hours.
6. the method for claim 1, wherein strengthens described extraction by the extraction intensifying technology that is selected from supersound process, heating, stirring, increase pressure and/or is exposed to quantity of radiant energy.
7. the method for claim 1, wherein removes described polar organic solvent by evaporation.
8. the method for claim 1, wherein said step of transesterification comprises:
Under the existence of acidity or basic catalyst, make described oil contact with alcohol.
9. method as claimed in claim 8, wherein said alcohol is the alcohol that contains no more than 4 carbon atoms.
10. method as claimed in claim 9, wherein said an acidic catalyst is selected from sulfonic acid, H 2sO 4, HC1, Acetyl Chloride 98Min. and BF 3.
11. methods as claimed in claim 9, wherein said basic catalyst is selected from KOH, NaOH, NaOCH 3, Na 2cH 2cH 3and guanidine.
12. the method for claim 1 are wherein carried out described step of transesterification after described solvent is removed step.
13. the method for claim 1, the tobacco of wherein being planted by water planting obtains described tobacco biomass.
14. methods as claimed in claim 13, wherein obtain described tobacco biomass by nanowatt Huoshan tobacco.
15. methods as claimed in claim 14, wherein said polar organic solvent is ethyl acetate.
16. methods as claimed in claim 15, are wherein used methyl alcohol and/or ethanol and sulfuric acid catalyst to carry out described step of transesterification.
17. methods as claimed in claim 16, also comprise the step of from described biofuel separated described methyl alcohol and/or ethanol.
18. methods as claimed in claim 18, also comprise the step that washes described biofuel with water.
CN201280065904.1A 2011-12-05 2012-12-04 Production of biofuel from tobacco plants Pending CN104136581A (en)

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