CN1952047B - Production process of biological diesel oil - Google Patents
Production process of biological diesel oil Download PDFInfo
- Publication number
- CN1952047B CN1952047B CN2005100475143A CN200510047514A CN1952047B CN 1952047 B CN1952047 B CN 1952047B CN 2005100475143 A CN2005100475143 A CN 2005100475143A CN 200510047514 A CN200510047514 A CN 200510047514A CN 1952047 B CN1952047 B CN 1952047B
- Authority
- CN
- China
- Prior art keywords
- reaction
- fatty acid
- oil
- accordance
- static mixer
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- 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
Landscapes
- Fats And Perfumes (AREA)
- Liquid Carbonaceous Fuels (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a producing method of biological diesel oil. It makes the animal oil (or esters), vegetable oil (or esters) and low-carbon alcohol carry out the eater exchanging reaction in static admixer to produce the biological diesel oil. Charge the animal oil (or esters), vegetable oil (or esters) and low-carbon alcohol into the static 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 under 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-efficiency appliance 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 CN1408701A 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 conventional equipment-static mixer, 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 static mixer 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 the static mixing unit according to the reaction metering than scope, under the transesterification reaction condition, react.
The present invention can 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 contains the organic amine material of 1～5 carbon atom.
Transesterification reaction is 30 ℃～150 ℃ of temperature ranges, and preferred 30 ℃～130 ℃, 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 (gauge pressure, down together), 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 static mixer that the present invention relates to can use various types of static mixers in the prior art, can be according to the scale and the operational condition scale of determining static mixer of device.Specifically can comprise standard or off-gauge static mixers such as SV type, SX type, SL type, SY type, SH type, SK type, SD type, and what preferentially select for use is the SK type static mixer of standard.For improving the mixed effect of static mixer, can between static mixer outlet and inlet, set up the material circulation, the recycle stock volumetric flow rate is 5%～500% of an inlet amount.Also can be by the volume space velocity Control Circulation amount of recycle stock, be 1～20h as the volume space velocity of recycle stock
-1
The inventive method adopts the production unit of static mixer as biofuel, because the effect of static mixer mixed cell, when making material and left-handed, the time and dextrorotation, constantly change flow direction, not only push central liquid stream to periphery, and push peripheral fluid to center, thereby cause good warp-wise mixed effect.The turning effort of material self meanwhile also can take place believing that element connects on the interface that, this perfect meridional circulation mixing effect, 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 adopts static mixer 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.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.
Description of drawings
Fig. 1 is a kind of static mixer structure synoptic diagram;
Fig. 2 is a reaction system continuous operation process schema of the present invention.
Embodiment
As shown in Figure 1, static mixer of the present invention does not have moving parts in the pipeline 3, has only stationary element 4, its stationary element 4 is to be welded by the left-handed and right-hand(ed)screw plate that several distortions 180 are spent, its principle of work is to make material impact stationary element 4 in pipeline 3, the time and left-handed, the time and dextrorotation, constantly change flow direction, not only push central liquid stream to periphery, and push peripheral fluid to center, thereby cause good warp-wise mixed effect.The turning effort of material self meanwhile also can take place believing that element connects on the interface that, and this perfect meridional circulation mixing effect makes oil and alcohol reach the purpose that mixes, thereby improved rate of mass transfer and transformation efficiency.
As shown in Figure 2, to participate in the material of reaction according to stoichiometric ratio, be input in the static mixer opening for feed 6 with high-pressure gear pump respectively, feed stream impacts stationary element 4 under pressure in pipeline 3, produce violent eddy current, thereby uniform mixing generation transesterification reaction, reaction mass under pressure then, constantly change flow direction, to discharge port 1,2 directions flow, entered among the tundish C by discharge port 2 effusive materials, in being recycled to static mixer opening for feed 5, logistics is impacted stationary element 4 again with fresh material under pressure in pipeline 3 by high-pressure gear pump, produce violent eddy current, thereby uniform mixing generation transesterification reaction again, reaction mass constantly changes flow direction under pressure then, to discharge port 1,2 directions flow, reaction mass directly carries out distillation procedure after discharge port 1 is discharged, 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 93% and purity and be the glycerine more than 80%.
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 test tank A, add methyl alcohol in test tank B, 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 static mixer volume
-1, also be to be 1h in the reaction times), Oleum Gossypii semen and methyl alcohol are squeezed in the static mixer with pump respectively, in static mixer, impact stationary element short mix generation transesterification reaction with recycle stock, recycle stock speed is 95% of 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), the GC-14B gas chromatograph analysis of Tianjin company is led in utilization, recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 89.8%.Static mixer is the SK type static mixer of standard.
Embodiment 2
According to the method for embodiment 1, just feeding rate is a static mixer volumetrical 1/2nd, and recycle stock speed is 150% of inlet amount.Pass through standing separation from the effusive reaction product of static mixer discharge port, obtain fatty acid ester phase (upper strata), the GC-14B gas chromatograph analysis of Tianjin company is led in utilization, and recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 91.8%.
Embodiment 3
According to the method for embodiment 1, feeding rate is the ratio of static mixer volumetrical 1/4th, and recycle stock speed is 55% of inlet amount.Pass through standing separation from the effusive reaction product of static mixer discharge port, obtain fatty acid ester phase (upper strata), the GC-14B gas chromatograph analysis of Tianjin company is led in utilization, and recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 92.5%.
Embodiment 4
According to the method for embodiment 1, feeding rate is the ratio of static mixer volumetrical 1/5th, and recycle stock speed is 400% of inlet amount.Pass through standing separation from the effusive reaction product of static mixer discharge port, obtain fatty acid ester phase (upper strata), the GC-14B gas chromatograph analysis of Tianjin company is led in utilization, and recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 93.5%.
Embodiment 5
According to the method for embodiment 1, feeding rate equals the volume of static mixer, no recycle stock.Pass through standing separation from the effusive reaction product of static mixer discharge port, obtain fatty acid ester phase (upper strata), the GC-14B gas chromatograph analysis of Tianjin company is led in utilization, and 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, static mixer adopts SY type standard static mixing tank, pass through standing separation from the effusive reaction product of static mixer discharge port, obtain fatty acid ester phase (upper strata), the GC-14B gas chromatograph analysis of Tianjin company is led in utilization, and recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 94.8%.
Embodiment 7
Method according to embodiment 1, just the mol ratio of methyl alcohol and Oleum Gossypii semen is 5, static mixer adopts SL type standard static mixing tank, pass through standing separation from the effusive reaction product of static mixer discharge port, obtain fatty acid ester phase (upper strata), the GC-14B gas chromatograph analysis of Tianjin company is led in utilization, and recording the fatty acid triglycercide transformation efficiency is 95%, and the fatty acid ester content of middle methyl esters mutually is 85.8%.
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 static mixer discharge port, obtain fatty acid ester phase (upper strata), the GC-14B gas chromatograph analysis of Tianjin company is led in utilization, 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 static mixer discharge port, obtain fatty acid ester phase (upper strata), the GC-14B gas chromatograph analysis of Tianjin company is led in utilization, recording the fatty acid triglycercide transformation efficiency is 85%, 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 static mixer discharge port, obtain fatty acid ester phase (upper strata), the GC-14B gas chromatograph analysis of Tianjin company is led in utilization, 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), the GC-14B gas chromatograph analysis of Tianjin company is led in utilization, and 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 0.65MPa, passes through standing separation from the effusive reaction product of static mixer discharge port, obtain fatty acid ester phase (upper strata), the GC-14B gas chromatograph analysis of Tianjin company is led in utilization, and 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), the GC-14B gas chromatograph analysis of Tianjin company is led in utilization, and 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 1, it is the diethylamine of adding 0.1% in raw material, pass through standing separation from the effusive reaction product of static mixer discharge port, obtain fatty acid ester phase (upper strata), the GC-14B gas chromatograph analysis of Tianjin company is led in utilization, recording the fatty acid triglycercide transformation efficiency is 100%, and the fatty acid ester content of middle methyl esters mutually is 93.5%.
Embodiment 15
Method according to embodiment 12, just change rapeseed oil into soybean salad oil, the diethylamine of adding 1% in raw material, equal the volume of static mixer from feeding rate, the effusive reaction product of static mixer discharge port obtains fatty acid ester phase (upper strata) by standing separation, utilizes 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 95.5%.
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 (9)
1. the production method of a biofuel, comprise following content: adopt the reactor of static mixer 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 the static mixing unit according to the reaction metering than scope, between static mixer outlet and inlet, set up the material circulation, recycle stock speed is 5%～500% of inlet amount, reacts under the transesterification reaction condition.
2. in accordance with the method for claim 1, it is characterized in that adding catalyst for ester exchange reaction in reaction raw materials, the add-on of catalyzer is below 1.0% of raw material weight.
3. in accordance with the method for claim 1, it is characterized in that described transesterification reaction temperature is 30 ℃～150 ℃, the pressure normal pressure is to the vapour pressure of lower molecular weight monohydroxy-alcohol.
4. in accordance with the method for claim 1, it is characterized in that described transesterification reaction temperature is 30 ℃～130 ℃.
5. in accordance with the method for claim 1, it is characterized in that described transesterification reaction temperature is 60 ℃～100 ℃.
6. in accordance with the method for claim 1, it is characterized in that the described transesterification reaction time is 0.5～5h.
7. in accordance with the method for claim 1, it is characterized in that described transesterification reaction pressure is that normal pressure is to 1.0MPa.
8. in accordance with the method for claim 1, the mol ratio that it is characterized in that described monohydroxy-alcohol and animal oil or Tallow, beef, vegetables oil or vegetable tallow is 3～50.
9. in accordance with the method for claim 1, the mol ratio that it is characterized in that described monohydroxy-alcohol and animal oil or Tallow, beef, vegetables oil or vegetable tallow is 5～15.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2005100475143A CN1952047B (en) | 2005-10-19 | 2005-10-19 | Production process of biological diesel oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2005100475143A CN1952047B (en) | 2005-10-19 | 2005-10-19 | Production process of biological diesel oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1952047A CN1952047A (en) | 2007-04-25 |
| CN1952047B true CN1952047B (en) | 2010-04-21 |
Family
ID=38058608
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2005100475143A Active CN1952047B (en) | 2005-10-19 | 2005-10-19 | Production process of biological diesel oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1952047B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101338212B (en) * | 2007-07-05 | 2012-02-15 | 中国石油化工股份有限公司 | Method for preparing biodesel |
| CN101781609A (en) * | 2010-03-03 | 2010-07-21 | 北京国力源高分子科技研发中心 | Method for preparing biodiesel from hemp plant oil |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN1654601A (en) * | 2005-02-24 | 2005-08-17 | 浙江工业大学 | Method for preparing biological diesel oil |
-
2005
- 2005-10-19 CN CN2005100475143A patent/CN1952047B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN1654601A (en) * | 2005-02-24 | 2005-08-17 | 浙江工业大学 | Method for preparing biological diesel oil |
Non-Patent Citations (3)
| Title |
|---|
| 徐桂转.生物柴油的研究与进展.华中农业大学学报24 6.2005,24(6),644-650. * |
| 梁斌.生物柴油的生产技术.化工进展24 6.2005,24(6),577-585. |
| 梁斌.生物柴油的生产技术.化工进展24 6.2005,24(6),577-585. * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1952047A (en) | 2007-04-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Simasatitkul et al. | Reactive distillation for biodiesel production from soybean oil | |
| US7695533B2 (en) | Method for transesterifying vegetable oils | |
| CN101314719B (en) | Method for preparing biological diesel oil with series double-fixed bed and catalysis of solid catalyst | |
| CN100590176C (en) | Ester interchange method for producing bio-diesel oil | |
| CN100537711C (en) | A kind of production method of biofuel | |
| US7622600B1 (en) | System and method for the continuous production of bio-diesel | |
| CN100410349C (en) | Method for producing biological diesel oil through homogeneous successive reaction | |
| CN101619329A (en) | Technical method for preparing biodiesel by biocatalysis one-pot method | |
| CN101177617B (en) | Process for preparing biodiesel | |
| CN100360644C (en) | Production process of biological diesel | |
| CN100392045C (en) | Method of synthesizing biodiesel oil using fixed bed gaseous phase esterification reaction | |
| CN101829528B (en) | Hydrolysis tower for oil and fat hydrolysis and method for oil hydrolysis by using same | |
| CN1952048B (en) | Production process of biological diesel oil | |
| CN1952047B (en) | Production process of biological diesel oil | |
| CN201125231Y (en) | Mobile biological diesel oil production facility | |
| CN101402873A (en) | Method for producing light biological diesel oil with seed oil of camphor | |
| CN1900224B (en) | Process for preparing biological diesel oil | |
| CN101280209B (en) | Method for continuous production of biodiesel | |
| CN101768517A (en) | Preparation method of biodiesel | |
| US20080249325A1 (en) | Method and Device For Continuous Process of Transesterification of Carboxylic Acid Esters in a Supercritical Monovalent Alcohol | |
| CN101037621A (en) | Production technique of automotive harmonic biodiesel | |
| CN111411024A (en) | Method and device for producing biodiesel by micro-reaction ester exchange | |
| KR100811625B1 (en) | Preparing method of alkyl ester | |
| CN101250425B (en) | Method for preparing bio-diesel oil by employing annular-pipe reactor | |
| CN103881827B (en) | A kind of bio-oil prepares the method for biofuel |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |