CN1952048B - Production process of biological diesel oil - Google Patents
Production process of biological diesel oil Download PDFInfo
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- CN1952048B CN1952048B CN2005100475158A CN200510047515A CN1952048B CN 1952048 B CN1952048 B CN 1952048B CN 2005100475158 A CN2005100475158 A CN 2005100475158A CN 200510047515 A CN200510047515 A CN 200510047515A CN 1952048 B CN1952048 B CN 1952048B
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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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- 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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- 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
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Abstract
The invention relates to a producing process of biological diesel oil by making the animal oil (or esters), vegetable oil (or esters) and low-carbon alcohol carry out the eater exchanging reaction in striking admixer to produce the biological diesel oil. Charge the animal oil (or esters), vegetable oil (or esters) and low-carbon alcohol into the striking admixer according to the reacting ratio, control the temperature and pressure of the admixer to make the materials mix and react quickly. The invention can be used in successive production and has high transformation efficiency in malacipeous conditions. Compared to the present technologies, the invention has the advantages of simple procedures, malacipeous conditions, high transformation efficiency and less by-products; besides, the invention can be used to produce diesel oil with different kinds of animal oil (or esters) and vegetable oil (or esters).
Description
Technical field
The present invention relates to a kind of production method of biofuel, particularly adopt high efficient mixed reactor production method of bio-diesel oil.
Background technology
Fatty acid triglyceride, particularly animal and plant fat and oil carry out the monoester that transesterification reaction obtains with the lower molecular weight monohydroxy-alcohol, to the diesel oil that obtains from petroleum fractions similar character are arranged, can be used as fuel and use, generally the fuel that will obtain in this way is called biofuel.
The biofuel of producing by greasy transesterification reaction has the following advantages: 1) good environmental protection characteristic is arranged.The biofuel sulphur content is low, does not contain the aromatic hydrocarbon that environment is polluted.2) engine cold-starting performance is preferably arranged, additive-free condensation point reaches-20 ℃.3) lubricity is preferably arranged, can reduce the wear rate of oil injection pump, engine cylinder-body and connecting rod, prolong its work-ing life.4) good safety performance is arranged, its flash-point height does not belong to hazardous substance.5) good fuel performance is arranged, its cetane value height, combustionproperty is better than ordinary diesel oil.6) has recyclability.Biofuel is as a kind of renewable energy source, and its resource can be inexhausted.
At present, mainly adopt chemical ester-interchange method production biofuel, use acid, alkali and molecular sieve as catalyzer.When using alkali (organic bases or mineral alkali), when alkali concn is too high, can cause side reaction to take place as catalyzer.Alkali and product carry out saponification reaction, cause productive rate to descend.When using acid as catalyzer, need higher temperature, the acid-catalyzed transesterification reaction is a reversible.Power consumption height and yield are low.When using molecular sieve as catalyzer, need carry out transesterification reaction under higher temperature of reaction, this moment, methyl alcohol was vapor state, was unfavorable for the carrying out that reacts.No matter adopt the sort of catalyzer, all there is following shortcoming in aforesaid method: complex process, alcohol must be excessive, and subsequent technique must have corresponding pure retrieving arrangement, energy consumption height; Product color is dark, because unsaturated fatty acids is at high temperature apt to deteriorate in the fat; Esterification products is difficult to reclaim the cost height; Discharging of waste liquid is arranged in the production process.In addition, in the prior art ester that obtains of reaction mutually in, purpose product (as methyl esters) content lower (being generally 50%～70%), must a large amount of monoglycerides and triglyceride be looped back reactor by separating, in fact cause the reactor utilization ratio to reduce, the raw material processing power descends, and production efficiency is lower.
In order to solve the problem of discharging of waste liquid in the production process, people bring into use the biological enzyme biodiesel synthesis, and this method has mild condition, and pure consumption is little, advantages such as non-pollution discharge.Shortcoming is: greasy transformation efficiency is low; The work-ing life of enzyme is short; Product is difficult to separate with glycerine; Lipase price height; Therefore there is not industrial application value.
In order to solve the problem of catalyst separating, Chinese patent CN1408701A discloses a kind of method and apparatus for preparing fatty acid ester.Under the condition of supercritical state and catalyzer existence, use the reactor of this invention, prepare fatty acid ester.Wherein reactor is returned in the reaction mixture recirculation that contains unreacted reactant and/or intermediate product.The preferred temperature of this method is 240 ℃～400 ℃, and preferred temperature is 245 ℃～350 ℃, and preferred reaction pressure is 0.5MPa～25MPa, and preferred reaction pressure is 2MPa～22MPa, preferred especially 8MPa～20MPa.This method has increased the reaction interface area, has improved transformation efficiency.Chinese patent CN1626621A also discloses a kind of method of fatty acid ester and fuel of fatty acid esters of preparing.This fatty acid ester is in the presence of catalyst-free, grease and alcohol both one of be under the condition of supercritical state, grease and pure prepared in reaction.This method preferable reaction temperature is no more than 400 ℃, and preferred reaction pressure is 0.4MPa～25.0MPa.There is not the problem of catalyst separating in this method, and product need not circulate, so energy consumption is low.But because above two kinds of methods are all being carried out, can cause the cracking of animal and plant grease under High Temperature High Pressure, have the high problem of cost of equipment simultaneously.
Japanese Patent (spy opens 2002-167356) also discloses a kind of preparation method of fatty acid ester, this method is to adopt a kind of volatile organic amine as catalyzer, relatively preparing fatty acid ester under the demulcent condition, from technological angle, do not need separating catalyst, can simply make with extra care out fatty acid ester, and avoid existing in the traditional method glycerine problem of middle catalyst residue mutually that is separated.The optimum reaction condition of this method is that 60～150 ℃ of temperature of reaction, reaction pressure are 0.2～0.9MPa.Though this method has solved the separation problem of catalyzer, but still it is poor with animal and plant grease mutual solubility to exist alcohol, and reaction system is two-phase, and transesterification reaction is only carried out the problem that speed of reaction is low at the interface.
In order to improve transformation efficiency, Chinese patent CN1496398A discloses a kind of method that obtains fatty acid ester by alcoholysis from the triacylglycerol ester.In order to accelerate ester-exchange reaction, add a certain amount of at least a alkanol fatty acid ester in initial reaction phase, especially monobasic chain triacontanol ester, preferred methyl esters, ethyl ester and/or ethyl ester, in fat that pending transesterify is arranged and/or oil, so that the reaction mixture that generates thus is made of single-phase.Thereby make this process just keep high reaction rate from beginning.And solved the problem of lipid acid to the reaction conversion ratio influence.Because the starting stage of transesterify can be avoided or shorten to this method, shortened the reaction times, but the selectivity and the transformation efficiency of transesterification reaction there is not too big contribution; Reaction needed is carried out cyclical operation, has increased energy consumption; The selected catalyzer price of reaction process height; Ester-exchange reaction itself generates water, and water is poisonous to reacting selected catalyzer, so catalyst life is short; The catalytic activity salt that is insoluble to reaction mixture will be deposited on the carrier, and catalyzer is made and/or the sepn process complexity.
Summary of the invention
At the deficiencies in the prior art, the invention provides a kind of use impact flow reactor, the novel method of continuous production biofuel.Under the demulcent reaction conditions, reached high transformation efficiency.Avoided catalyst separating, it is poor with animal and plant grease mutual solubility to have solved alcohol, and reaction system is two-phase, and transesterification reaction is only carried out the problem that speed of reaction is low at the interface.Simplify technical process, reduced production cost and facility investment.Not having discharging of waste liquid in the production process, is an environmental protection processing method.
The production process of biofuel of the present invention comprises following content: adopt the reactor of impact flow reactor as transesterify, with animal and vegetable oil or fat that contains fatty acid triglycercide and the monohydroxy-alcohol with 1～8 carbon atom is raw material, feed premix tank according to the reaction metering than scope, carry out pre-mixing at premix tank, squeeze into the opening for feed on impact flow reactor both sides then respectively by equipment for liquid transportation, reaction product is discharged impact flow reactor.
In impact flow reactor, material moves to the middle part by guide shell, and clashes in opposite directions at this place, forms impingement region around impact surface reaches.In this district from relative movement violent between the stream of different directions group make between stream group with liquid phase between effectively mix and contact the promotion transesterification reaction.Behind the bump, fluid returns the two ends, the left and right sides of container respectively through the ring casing between guide shell and container inner wall, be fed respectively again then carry pass through about two guide shells flow to middle part and bump, circulation so repeatedly once more.Make oil and alcohol reach the purpose that mixes, thereby improved rate of mass transfer, under demulcent reaction conditions and higher transformation efficiency, realize the continuous production method of bio-diesel oil.
The present invention does not use catalyzer, and the so-called catalyzer that do not use is meant: do not use catalyzer or use indivisible catalyzer, for example the add-on of catalyzer is below 1.0% (weight) of raw material.Do not use catalyzer to mean that technological process is simple, production cost is low.Here the catalyzer of indication is the organic amine material.As contain the organic amine material of 1～5 carbon atom.
Transesterification reaction is 30 ℃～130 ℃ of temperature ranges, and preferred 30 ℃～120 ℃, what override was selected is to carry out between 60 ℃～100 ℃.Reaction is to carry out to the pressure of the vapour pressure of lower molecular weight monohydroxy-alcohol at normal pressure.
Any fatty acid glyceryl ester can be made raw material of the present invention, and especially preferred is to have 10～22 carbon atoms with in animal and plant fat and/or the oil, particularly those fatty acid radicals, and preferably 12～18 carbon atoms makes raw material.As the example of vegetable raw material can enumerate soybean oil, rapeseed oil, sunflower seed oil, peanut oil, Oleum Gossypii semen, plam oil, Semen Lini oil, Viscotrol C, beet oil and olive wet goods one or more.The example of animal raw materials such as butter, lard one or both.
The present invention uses lower molecular weight monohydroxy-alcohol and fatty acid glyceryl ester with 1～8 carbon atom to carry out transesterification reaction.The alcohol that preferably has 1～6 carbon atom, special particular methanol or ethanol.
The concrete reaction times among the present invention is depended on the raw material-grease that adopted and kind, reaction conditions and the desired yield of alcohols material, and the general reaction times carries out between 0.5～5h.
According to the present invention, transesterification reaction is to carry out under the pressure between the vapour pressure of selected alcohol at normal pressure.Generally arrive 1.0MPa, preferred 0.10MPa～0.8MPa at normal pressure.Suitable pressure can increase the reaction interface area, improves greasy transformation efficiency.
According to implementation method of the present invention, the mol ratio that transesterification reaction is chosen lower molecular weight monohydroxy-alcohol and animal and plant fat and oil is 3～50, and is preferred 5～30, and what override was selected is 5～15.But find that by test when the add-on of monohydroxy-alcohol was slightly larger than theoretical amount, the selectivity of reaction and transformation efficiency all had raising.
The impact flow reactor that the present invention relates to can use and be used for liquid reactive various types of impact flow reactor in the prior art, can be according to the scale and the operational condition scale of determining impact flow reactor of device.For example preferably use the impact flow reactor of Fig. 1.For improving the mixed effect of impact flow reactor, can between impact flow reactor outlet and inlet, set up the material circulation, the recycle stock amount is 5%～500% of an inlet amount.
The present invention finds that by the Reaction Mechanisms in the research production of biodiesel low mass molecule alcohol is poor with moving value thing grease mutual solubility in the production of biodiesel, and reaction system is two-phase, and transesterification reaction is only carried out at the interface, is the main raw material that causes reaction efficiency lower.Therefore, the present invention adopts impact flow reactor as transesterification reactor, has strengthened microcosmic greatly and has mixed and the microcosmic mass transfer, under the demulcent reaction conditions, has reached high transformation efficiency.Avoid catalyst separating, efficiently solved the problems referred to above.Simplify technical process, reduced production cost and facility investment.Not having discharging of waste liquid in the production process, is an environmental protection processing method.
Description of drawings
Fig. 1 is that the present invention adopts the impact flow reactor structural representation;
Fig. 2,3,4,5 is reaction system continuous operation process schematic flow sheet of the present invention.
Embodiment
As shown in Figure 1, impact flow reactor of the present invention comprises: locate and be submerged in the material two guide shells 3,5 and coaxial respectively and be installed in two feed-pipes 1,6 in two guide shells symmetrically to being installed in nearly two ends, container 4 middle parts respectively with becoming.The process stream of packing in the container 1 is the useful volume district of reaction, in order to improve flow efficiency, the cylindrical shell making that container 4 usefulness are circular.Under the promotion of the material of material in two feed-pipes in the guide shell respectively from two ends through guide shell 3,5 high speed flow to container 4 centers, and clash in opposite directions in the center, around impact surface, form impingement region.In this district from relative movement violent between the stream of different directions group make between stream group with liquid phase between effectively contact and mix, carry out transesterification reaction.Behind the bump, fluid returns two ends through the ring casing between guide shell 3,5 and container 4 inwalls, and the mass transport that is fed again then in the pipe 1,7 flows to container 4 centers and bump, circulation so repeatedly once more by guide shell 3,5.Meanwhile transesterification reaction also can take place in material on impact surface, and this perfect mixing effect of circulation in opposite directions makes oil and alcohol reach the purpose that mixes, thereby improved rate of mass transfer and transformation efficiency.The recycle stock handling equipment (as pump) of impact flow reactor can adopt one or several.
As Fig. 2,3,4, shown in 5, to participate in the material of reaction according to stoichiometric ratio, with pump or other equipment for liquid transportation material is input among premix tank D or the tundish C respectively, carry out pre-mixing, then by pump or other equipment for liquid transportation, be input to the opening for feed 1 of impact flow reactor, 7, feed stream under pressure high speed through guide shell 3,5 flow to container 4 centers, and clash in opposite directions in the center, around impact surface, form impingement region, material behind the process bump is from two side outlets 2,6 flow to tundish C, be input to the opening for feed 1 of impact flow reactor again by pump, 7, clash into once more, come controlling reactor pressure by pressure-regulator A, thus uniform mixing generation transesterification reaction.The reaction mass of discharging from pressure-regulator A directly carries out distillation procedure, unreacted alcohols material can be separated, and recycles then.Through the reaction product after the distillation, standing separation, the upper strata ester promptly can be used as the biofuel product mutually and uses, and lower floor is that the glycerine of purity more than 80% can be used as the byproduct sale.Sometimes the reaction product of discharging continuously is without above-mentioned distillation procedure, and direct standing separation can obtain purity and be biofuel product more than 95% and purity and be the glycerine more than 80%.
Further specify method of the present invention and effect below by embodiment and comparative example.
Further specify method of the present invention and effect below by embodiment and comparative example.The percentage composition that relates to is the quality percentage composition.
Embodiment 1
Add Oleum Gossypii semen in storage tank E, add methyl alcohol in storage tank F, the mol ratio of methyl alcohol and Oleum Gossypii semen is 10, and it (is that the feed volume air speed is 1h that the feeding rate of Oleum Gossypii semen and methyl alcohol equals the percussion flow reaction volume
-1, also be to be 1h in the reaction times), Oleum Gossypii semen and methyl alcohol are squeezed in the tundish C with pump respectively, with recycle stock pre-mixing in tundish, squeeze into impact flow reactor by pump then, transesterification reaction takes place by bump, the recycle stock amount is 95% of an inlet amount.Control reaction temperature is 130 ℃, reaction pressure is 0.8MPa, pass through standing separation from the effusive reaction product of static mixer discharge port, obtain fatty acid ester phase (upper strata), utilize the 6890N gas chromatograph analysis of Agilent company, recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 91.1%.Impact flow reactor is the impact flow reactor of Fig. 1.
According to the method for embodiment 1, just feeding rate is 1/2nd of an impact flow reactor, and the recycle stock amount is 75% of an inlet amount.Pass through standing separation from the effusive reaction product of impact flow reactor discharge port, obtain fatty acid ester phase (upper strata), utilize the 6890N gas chromatograph analysis of Agilent company, recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 93.8%.
Embodiment 3
According to the method for embodiment 1, feeding rate is the ratio of impact flow reactor volumetrical 1/4th, and recycle stock speed is 150% of inlet amount.Pass through standing separation from the effusive reaction product of impact flow reactor discharge port, obtain fatty acid ester phase (upper strata), utilize the 6890N gas chromatograph analysis of Agilent company, recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 94.5%.
According to the method for embodiment 1, feeding rate is the ratio of impact flow reactor volumetrical 1/5th, and recycle stock speed is 400% of inlet amount.Pass through standing separation from the effusive reaction product of impact flow reactor discharge port, obtain fatty acid ester phase (upper strata), utilize the 6890N gas chromatograph analysis of Agilent company, recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 95.8%.
Embodiment 5
According to the method for embodiment 1, feeding rate is the ratio of impact flow reactor volumetrical 1/2nd, and recycle stock speed is for being 5% of inlet amount.Pass through standing separation from the effusive reaction product of impact flow reactor discharge port, obtain fatty acid ester phase (upper strata), utilize the 6890N gas chromatograph analysis of Agilent company, recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 85.8%.
Embodiment 6
Method according to embodiment 1, just the mol ratio of methyl alcohol and Oleum Gossypii semen is 15, impact flow reactor adopts disclosed vertical circulation impact flow reactor among the CN 2659539Y, pass through standing separation from the effusive reaction product of impact flow reactor discharge port, obtain fatty acid ester phase (upper strata), utilize the 6890N gas chromatograph analysis of Agilent company, recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 90.8%.
Embodiment 7
Method according to embodiment 1, just the mol ratio of methyl alcohol and Oleum Gossypii semen is 5, impact flow reactor is adopted disclosed sinking circulation impact flow reactor among the CN2455353Y, pass through standing separation from the effusive reaction product of impact flow reactor discharge port, obtain fatty acid ester phase (upper strata), utilize the 6890N gas chromatograph analysis of Agilent company, recording the fatty acid triglycercide transformation efficiency is 95%, and the fatty acid ester content of middle methyl esters mutually is 89.8%.
Embodiment 8
Method according to embodiment 1, it is 100 ℃ just with temperature of reaction, pass through standing separation from the effusive reaction product of impact flow reactor discharge port, obtain fatty acid ester phase (upper strata), utilize the 6890N gas chromatograph analysis of Agilent company, recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 87.8%.
Embodiment 9
Method according to embodiment 1, it is 60 ℃ just with temperature of reaction, pass through standing separation from the effusive reaction product of impact flow reactor discharge port, obtain fatty acid ester phase (upper strata), utilize the 6890N gas chromatograph analysis of Agilent company, recording the fatty acid triglycercide transformation efficiency is 90%, and the fatty acid ester content of middle methyl esters mutually is 85.8%.
Embodiment 10
Method according to embodiment 1, just change methyl alcohol into ethanol, pass through standing separation from the effusive reaction product of impact flow reactor discharge port, obtain fatty acid ester phase (upper strata), utilize the 6890N gas chromatograph analysis of Agilent company, recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle ethyl ester mutually is 90.3%.
Embodiment 11
Method according to embodiment 1, just change methyl alcohol into ethanol, ethanol and greasy mol ratio are 15, temperature of reaction is 120 ℃, and reaction pressure is 0.5MPa, passes through standing separation from the effusive reaction product of static mixer discharge port, obtain fatty acid ester phase (upper strata), utilize the 6890N gas chromatograph analysis of Agilent company, recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle ethyl ester mutually is 94.5%.
Embodiment 12
Method according to embodiment 1, just change oleum gossypii seminis into rape seed oil, the feeding rate of rape seed oil is 1/4th of a static mixer volume, temperature of reaction is 130 ℃, and reaction pressure is 0.7MPa, passes through standing separation from the effusive reaction product of static mixer discharge port, obtain fatty acid ester phase (upper strata), utilize the 6890N gas chromatograph analysis of Agilent company, recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 92.5%.
Embodiment 13
Method according to embodiment 1, just change oleum gossypii seminis into soybean oil, the feeding rate of soybean oil is 1/2nd of a static mixer volume, temperature of reaction is 100 ℃, and reaction pressure is 0.4MPa, passes through standing separation from the effusive reaction product of static mixer discharge port, obtain fatty acid ester phase (upper strata), utilize the 6890N gas chromatograph analysis of Agilent company, recording the fatty acid triglycercide transformation efficiency is 95%, and the fatty acid ester content of middle methyl esters mutually is 93.5%.
Embodiment 14
Method according to embodiment 12, it is the diethylamine of adding 1% in raw material, pass through standing separation from the effusive reaction product of impact flow reactor discharge port, obtain fatty acid ester phase (upper strata), utilize the 6890N gas chromatograph analysis of Agilent company, recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 94.5%.
Embodiment 15
Method according to embodiment 12, just change rapeseed oil into soybean salad oil, the raw material feeding rate equals the static mixer volume, and the diethylamine of adding raw material 1%, by standing separation, obtain fatty acid ester phase (upper strata) from the effusive reaction product of impact flow reactor discharge port, utilize the 6890N gas chromatograph analysis of Agilent company, recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 95.8%.
Comparative example 1
Soybean salad oil 100 gram, methyl alcohol 50 grams, diethylamine 20 grams, water 10 grams are joined in 500 milliliters of withstand voltage glass flask, stir, be heated to 130 ℃ with the stirring velocity of 700rpm, this moment gauge pressure 0.65MPa.Continue down to stir at 130 ℃, reacted 3 hours.React and finish the back by standing separation, obtain fatty acid ester phase (upper strata), utilize the GC-14B gas chromatograph analysis of leading Tianjin company, recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 92%.
Comparative example 2
Press comparative example 1 method, just catalyzer diethylamine add-on is 2 grams.Product fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 90%.From comparative example 2 and embodiment 15 as can be seen, under the close situation of catalyst levels, the inventive method can reach better reaction effect (increase of purpose product selectivity) in the short reaction times, improved production efficiency greatly.
Comparative example 3
Press comparative example 1 method, just do not add the catalyzer diethylamine, raw material is an Oleum Gossypii semen, presses the proportioning raw materials of embodiment 1.Product fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 88.5%.Comparative example 3 is compared with embodiment 1, and under the situation of not using catalyzer, the inventive method can reach better reaction effect in the shorter reaction times.
Claims (10)
1. the production method of a biofuel, comprise following content: adopt the reactor of impact flow reactor as transesterify, with animal oil or Tallow, beef, vegetables oil or vegetable tallow that contains fatty acid triglycercide and the monohydroxy-alcohol with 1～8 carbon atom is raw material, feed premix tank according to the reaction metering than scope, carry out pre-mixing at premix tank, squeeze into the opening for feed on impact flow reactor both sides then respectively by equipment for liquid transportation, reaction product is discharged impact flow reactor.
2. in accordance with the method for claim 1, the temperature that it is characterized in that transesterification reaction is 30 ℃～130 ℃.
3. in accordance with the method for claim 1, it is characterized in that described transesterification reaction carries out to the pressure of the vapour pressure of lower molecular weight monohydroxy-alcohol at normal pressure.
4. in accordance with the method for claim 1, it is characterized in that described monohydroxy-alcohol is methyl alcohol or ethanol.
5. in accordance with the method for claim 1, it is characterized in that the described transesterification reaction time is that the reaction times is at 0.5～5h.
6. in accordance with the method for claim 1, it is characterized in that described transesterification reaction pressure is 0.10MPa～0.8MPa.
7. in accordance with the method for claim 1, the mol ratio that it is characterized in that described transesterification reaction monohydroxy-alcohol and animal oil or Tallow, beef, vegetables oil or vegetable tallow is 3～50.
8. in accordance with the method for claim 1, the mol ratio that it is characterized in that described transesterification reaction monohydroxy-alcohol and animal oil or Tallow, beef, vegetables oil or vegetable tallow is 5～15.
9. in accordance with the method for claim 1, it is characterized in that setting up the material circulation between impact flow reactor outlet and inlet, the recycle stock amount is 5%～500% of an inlet amount.
10. in accordance with the method for claim 1, it is characterized in that containing in the transesterification reaction raw material organic amine catalyzer of weight content below 1.0%.
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| CN101085924B (en) * | 2007-06-11 | 2010-05-26 | 浙江工业大学 | Technique and device for catalyzing biomass fast thermal cracking by high temperature ironic liquid |
| CN103785330B (en) * | 2012-11-01 | 2016-01-20 | 中国石油化工股份有限公司 | A kind of application of olefin hydration reactor |
| CN109486504B (en) * | 2017-09-09 | 2021-01-05 | 中国石油化工股份有限公司 | Improver for improving lubricity of low-sulfur diesel oil and synthetic method thereof |
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| CN1117063C (en) * | 1997-11-24 | 2003-08-06 | 能源环境技术股份有限公司 | Method and equipment for producing fatty acid methyl ester |
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