CN1923959A - Method of preparing organism diesel oil from mixing plant oil - Google Patents
Method of preparing organism diesel oil from mixing plant oil Download PDFInfo
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- CN1923959A CN1923959A CNA2005100937890A CN200510093789A CN1923959A CN 1923959 A CN1923959 A CN 1923959A CN A2005100937890 A CNA2005100937890 A CN A2005100937890A CN 200510093789 A CN200510093789 A CN 200510093789A CN 1923959 A CN1923959 A CN 1923959A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- 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
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Abstract
The invention discloses a preparing method of biological diesel based on composite plant oil as raw material, which is characterized by the following: blending low-acid plant oil with acid less than 5mgKOH/g, crude oil with acid value at 20-110mgKOH/g and C1-8 monohydric alcohol; reacting at 200-320 deg.c under 5-12Mpa; setting the molar rate of alcohol and oil at 3-60:1; collecting fatty acid ester; setting the weight rate of low-acid plant oil and crude oil at 1:0.02-50.
Description
Invention field
The present invention relates to a kind of by grease and monohydroxy-alcohol prepared in reaction method of bio-diesel oil.
Background technology
Biofuel can be by grease and C
1-C
8Monohydroxy-alcohol carry out transesterification reaction and make, it (generally is low-carbon alcohol, as C with another kind of alcohol that transesterification reaction refers to triglyceride level
1-C
8Monohydroxy-alcohol) reaction carried out.In its reaction product fatty acid ester is arranged, promptly biofuel, mono-glycerides, two sweet esters, glycerine, pure and mild triglyceride level are raw material.The preparation method of biofuel can be divided into acid catalyzed process, base catalysis method, enzyme catalysis method and supercritical methanol technology.
It is raw material that CN1473907A adopts the tankage of vegetable oil refining and edible refiltered oil, catalyzer is inorganic and organic acid is composite forms by sulfuric acid, hydrochloric acid, tosic acid, Witco 1298 Soft Acid, naphthene sulfonic acid etc., produce through operations such as acidifying removal of impurities, continuously dehydrating, esterification, layering, underpressure distillation, the pressure of continous vacuum dehydration is 0.08～0.09Mpa, 60～95 ℃ of temperature, dewater to water-content below 0.2%, esterif iotacation step catalyzer add-on 1～3%, 60～80 ℃ of esterification temperatures, 6 hours reaction times.Reaction after product neutralization is earlier removed catalyzer, and then, layering removes and anhydrates, and the after product that anhydrates obtains biofuel through underpressure distillation.
Be that slow of speed of response have a large amount of spent acid and produce more with acid catalysis and base catalysis than existing problems.
DE3444893 discloses a kind of method, use acid catalyst, normal pressure, 50～120 ℃, free fatty acids and alcohol being carried out esterification, oil plant is carried out pre-esterification treatment, is that catalyzer carries out transesterification reaction then with the alkali metal hydroxide, but the acid catalyst of leaving over will be neutralized by alkali, and the usage quantity of alkali metal hydroxide can increase.Adopt pre-esterification, make work flow elongated, facility investment, energy consumption significantly rises, and in addition, needs basic catalyst is removed from product, has a large amount of waste water to produce.Recovery glycerine difficulty.
CN1472280A discloses a kind of method, as acyl acceptor, carries out transesterification reaction production biofuel with biological enzyme as catalyzer with fatty acid ester.The deficiency that adopts enzyme catalyst to exist is: long reaction time, efficient are lower, and enzyme is more expensive, and in reaction easy inactivation.
CN1111591C discloses the method for a kind of grease and monohydroxy-alcohol prepared in reaction fatty acid ester, this method comprises methyl alcohol reacted with grease and obtains fatty acid ester, at 280 ℃, under the 12Mpa condition, the fatty acid methyl ester production rate is 60%, this patent is not open to mono-glycerides in the crude product after reacting, two sweet esters, and how triglyceride level is handled.
Summary of the invention
Experiment is found: when vegetables oil and monohydroxy-alcohol carry out transesterification reaction, the low general reactive behavior of acid number vegetables oil is lower, cause in the final product yield of biofuel lower, and the crude oil activity of higher acid value is higher, but when simple crude oil with higher acid value is the biofuel of feedstock production, the acid number of reacting coarse product is generally higher, is not easy to reach the requirement of biofuel standard.For overcoming above problem, the invention provides a kind of is the feedstock production method of bio-diesel oil with the mixed vegetable oil.
Preparation method of bio-diesel oil provided by the invention comprises: with the low acid number vegetables oil of acid number＜5mgKOH/g and crude oil and the C of acid number 20-110mgKOH/g
1-C
8Monohydroxy-alcohol mixes, at temperature of reactor 200-320 ℃, and pressure 5-12Mpa, alcohol/molar equivalent 3-60: react under 1 the condition, collect fatty acid ester.
Said low acid number vegetables oil can be treated oil or non-treated oil, and refining step can be in the operations such as matter, alkali refining, dephosphorization matter, decolouring, deodorization one or more of coming unstuck.
Said crude oil is meant that oilseeds only pass through squeezing or solvent extraction and do not pass through the vegetables oil that refining step obtains.The refining step operations such as matter, alkali refining, dephosphorization matter, decolouring, deodorization that include but not limited to come unstuck.
The weight ratio of low acid number vegetables oil and crude oil is 1: 0.02-50, preferred 1: 0.04-20, more preferably 1: 0.06-10.The content of crude oil is big more in the mixing oil, and the reactive behavior of mixing oil is high more, but after content was increased to a certain degree, the character with crude oil was identical substantially to mix oil properties.The kind of low acid number vegetables oil and two kinds of oil of crude oil can be identical, also can difference.
Said vegetables oil can be soybean oil, rapeseed oil, the various vegetables oil of palm wet goods or their mixture.
Said C
1-C
8The preferred unitary fatty alcohol of monohydroxy-alcohol, preferably methyl alcohol or ethanol.
Can also optionally add basic cpd in the reaction system as catalyzer.Described basic cpd is selected from IA in the periodictable, the oxyhydroxide of IIA element, alcoholate, oxide compound, carbonate, supercarbonate, C
12～C
24Soap, preferred sodium, potassium, magnesium, calcium, the oxyhydroxide of barium, alcoholate, oxide compound, carbonate, supercarbonate, soap, more preferably following compound: the oxyhydroxide of sodium, potassium, magnesium, oxide compound, alcoholate, C
12～C
24Soap.The add-on of basic cpd is 0.005～0.08% of a grease weight, preferred 0.008～0.05%.
Specifically, the inventive method can adopt tubular type or tank reactor, and tank reactor can have or not have stirring.Grease and alcohol can offer reactor separately, or with offering reactor after their mixing, before offering reactor, available preheater also can directly enter reactor, like this with the material preheating, reactor had both played the effect of preheater, also played the effect of reactor.As adopt preheater, preheating together after can or mixing grease and alcohol difference preheating.
In reaction process condition, temperature raises, and reaction conversion ratio is high more, because from the kinetics angle, temperature raises and to help reaction and carries out, but temperature is when being higher than 320 ℃, the reaction product color burn, there is heavies to produce, simultaneously, also can cause glycerine to decompose, therefore, temperature of reactor 200-320 ℃, preferably 240-280 ℃.
Pressure is high more favourable more to reaction, but pressure is too high, makes the investment of device and process cost raising more, so, pressure 5-12Mpa, preferably 6-10Mpa.
Monohydroxy-alcohol and greasy mol ratio can in very large range change, and methyl alcohol shortens material residence time in reactor with the too high meeting of mol ratio of oil, and transformation efficiency descends.Plant energy consumption and process cost are increased, usage ratio of equipment is descended.So alcohol/molar equivalent remains on alcohol: oil=3-60: 1, best 4-12: 1 (mol ratio).
The inventive method is that stock oil prepares biofuel with the mixing oil of low acid number oils and crude oil, overcome the high defective of crude oil product acid number of the active low and higher acid value of low acid number oils, the yield of biofuel is obviously improved, it with the mixing oil summation of the output of the biofuel of raw material output when being higher than the gross weight low acid number thing oil identical and crude oil far away and reacting separately with mixing oil, the acid number of product obviously descends simultaneously, is convenient to obtain the satisfactory biofuel of acid number by aftertreatment.
The inventive method adaptability to raw material is strong, and easy switching has adapted to vegetables oil diversity and seasonal characteristics.
Embodiment
Further specify the present invention below by example, but the present invention is not limited to this.
Comparative Examples 1
The refined soybean oil that with acid number is 1.4mgKOH/g is with 60 Grams Per Hours, the speed of methyl alcohol molar equivalent 5 continuously is provided in the tubular reactor, temperature is 280 ℃ in the reactor, pressure 9.5Mpa, reacting coarse product is behind separation of methanol, glycerine, rectification under vacuum steams fatty acid methyl ester, fatty acid methyl ester yield 47wt%.
Comparative Examples 2
With acid number is that the 0.9mgKOH/g rapeseed oil is with 60 Grams Per Hours, the speed of methyl alcohol molar equivalent 7 continuously is provided in the tubular reactor, in the reactor temperature 270-280 ℃, pressure 8Mpa, reacting coarse product is behind separation of methanol, glycerine, rectification under vacuum steams fatty acid methyl ester, fatty acid methyl ester yield 61wt%.
Embodiment 1
The hair vegetables oil that will contain unsaponifiables 1.2%, acid number 72mgKOH/g mixes by weight 0.3: 1 with the rapeseed oil of Comparative Examples 2, to mix oil plant with 60 Grams Per Hours, the speed of molar ratio of methanol to oil 7 continuously is provided in the tubular reactor, in the reactor temperature 270-280 ℃, pressure 8Mpa, reacting coarse product is behind separation of methanol, glycerine, and rectification under vacuum steams fatty acid methyl ester, fatty acid methyl ester yield 92.2wt%, acid number 3.5mgKOH/g.The residue raffinate can be used as raw material and is circulated to the reactor feed mouth at the bottom of the still, carries out secondary reaction.
Under identical condition, with acid number 72mgKOH/g the hair vegetables oil be raw material, fatty acid methyl ester yield 87.2wt%, acid number 9.0mgKOH/g.
Embodiment 2
To contain that refined soybean oil mixes by weight at 1: 1 in hair vegetables oil and the Comparative Examples 1 of unsaponifiables 1.5%, acid number 52mgKOH/g, to mix oil plant with 60 Grams Per Hours, the speed of molar ratio of methanol to oil 5 is provided in the tubular reactor, in the reactor temperature 270-280 ℃, pressure 8.5Mpa, reacting coarse product is behind separation of methanol, glycerine, rectification under vacuum steams fatty acid methyl ester, fatty acid methyl ester yield 91 ± 1wt%, acid number 3.3mgKOH/g, the residue raffinate can be used as raw material and is circulated to the reactor feed mouth at the bottom of the still, carries out secondary reaction.
Under identical condition, with acid number 52mgKOH/g the hair vegetables oil be raw material, fatty acid methyl ester yield 86wt%, acid number 7.2mgKOH/g.
Embodiment 3
The hair vegetables oil of acid number 28.5mgKOH/g is mixed by weight 1: 1: 1 with soybean oil, rapeseed oil, to mix oil plant with 60 Grams Per Hours, the speed of molar ratio of methanol to oil 5 continuously is provided in the tubular reactor, 320 ℃ of temperature of reactor, obtain fatty acid methyl esters under the condition of pressure 9Mpa, fatty acid methyl ester yield 83.9wt%, acid number＜2.0mgKOH/g, the residue raffinate can be used as raw material and is circulated to the reactor feed mouth at the bottom of the still, carries out secondary reaction.
Under identical condition, with acid number 28.5mgKOH/g the hair vegetables oil be raw material, fatty acid methyl ester yield 84.2wt%, acid number 4.7mgKOH/g.
Under identical condition, soybean oil, rapeseed oil are raw material, and the fatty acid methyl ester yield is respectively 69wt%, 76wt%.
Embodiment 4
Acid number is that the oil plant of 100mgKOH/g mixes by weight 0.1: 1 with the soybean oil of Comparative Examples 1, to mix oil plant with 60 Grams Per Hours, the speed of molar ratio of methanol to oil 10 continuously is provided in the tubular reactor, temperature is 320 ℃ in the reactor, pressure 9Mpa, and reacting coarse product is behind separation of methanol, glycerine, rectification under vacuum steams fatty acid methyl ester, fatty acid methyl ester yield 72wt%, the residue raffinate can be used as raw material and is circulated to the reactor feed mouth at the bottom of the still, carries out secondary reaction.
Under identical condition, be raw material with the soybean oil of Comparative Examples 1, fatty acid methyl ester yield 55wt%.
Embodiment 5
The hair vegetables oil of acid number 59mgKOH/g is mixed by weight 40: 1 with the rapeseed oil of Comparative Examples 2, to mix oil plant with 60 Grams Per Hours, the speed of molar ratio of methanol to oil 6 continuously is provided in the tubular reactor, in the reactor temperature 270-280 ℃, pressure 9～10Mpa, reacting coarse product is behind separation of methanol, glycerine, rectification under vacuum steams fatty acid methyl ester, fatty acid methyl ester yield 86wt%, the residue raffinate can be used as raw material and is circulated to the reactor feed mouth at the bottom of the still, carries out secondary reaction.
Claims (9)
1. be the feedstock production method of bio-diesel oil with the mixed vegetable oil, comprise: the low acid number vegetables oil of acid number＜5mgKOH/g and crude oil and the C of acid number 20-110mgKOH/g
4-C
8Monohydroxy-alcohol mixes, at temperature of reactor 200-320 ℃, and pressure 5-12Mpa, alcohol/molar equivalent 3-60: react under 1 the condition, collect fatty acid ester, the weight ratio of wherein low acid number vegetables oil and crude oil is 1: 0.02-50.
2. in accordance with the method for claim 1, it is characterized in that said crude oil is meant that oilseeds are through the vegetables oil that squeezes or solvent extraction obtains.
3. in accordance with the method for claim 1, it is characterized in that the weight ratio of low acid number vegetables oil and crude oil is 1: 0.04-20.
4. in accordance with the method for claim 3, it is characterized in that the weight ratio of low acid number vegetables oil and crude oil is 1: 0.06-10.
5. in accordance with the method for claim 1, it is characterized in that said C
1-C
8Monohydroxy-alcohol is a unitary fatty alcohol,
6. in accordance with the method for claim 5, it is characterized in that said C
1-C
8Monohydroxy-alcohol is methyl alcohol or ethanol.
7. in accordance with the method for claim 1, it is characterized in that temperature of reactor is 240-280 ℃.
8. in accordance with the method for claim 1, it is characterized in that pressure is 6-10Mpa.
9. in accordance with the method for claim 1, it is characterized in that alcohol/molar equivalent is 4-12: 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100937890A CN100460482C (en) | 2005-08-31 | 2005-08-31 | Method of preparing organism diesel oil from mixing plant oil |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100937890A CN100460482C (en) | 2005-08-31 | 2005-08-31 | Method of preparing organism diesel oil from mixing plant oil |
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| Publication Number | Publication Date |
|---|---|
| CN1923959A true CN1923959A (en) | 2007-03-07 |
| CN100460482C CN100460482C (en) | 2009-02-11 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005100937890A Active CN100460482C (en) | 2005-08-31 | 2005-08-31 | Method of preparing organism diesel oil from mixing plant oil |
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| CN (1) | CN100460482C (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102260596A (en) * | 2010-05-27 | 2011-11-30 | 中国石油化工股份有限公司 | Method for preparing biodiesel by two-step process |
| CN102260597A (en) * | 2010-05-27 | 2011-11-30 | 中国石油化工股份有限公司 | Preparation method of high purity biodiesel |
| CN101338212B (en) * | 2007-07-05 | 2012-02-15 | 中国石油化工股份有限公司 | Method for preparing biodesel |
| CN103013678A (en) * | 2011-09-20 | 2013-04-03 | 中国石油化工股份有限公司 | Method for reducing biodiesel crude product acid value, and biodiesel preparation method |
| CN103173281A (en) * | 2011-12-21 | 2013-06-26 | 中国石油化工股份有限公司 | Method for reducing acid value of biodiesel crude product and preparation method of biodiesel |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1197937C (en) * | 2002-08-07 | 2005-04-20 | 四川古杉油脂化学有限公司 | Process for producing biological diesel oil |
| CN1190471C (en) * | 2003-07-22 | 2005-02-23 | 清华大学 | Method for synthetizing biological diesel oil by oil and fat materials |
-
2005
- 2005-08-31 CN CNB2005100937890A patent/CN100460482C/en active Active
Cited By (9)
| 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 |
| CN102260596A (en) * | 2010-05-27 | 2011-11-30 | 中国石油化工股份有限公司 | Method for preparing biodiesel by two-step process |
| CN102260597A (en) * | 2010-05-27 | 2011-11-30 | 中国石油化工股份有限公司 | Preparation method of high purity biodiesel |
| CN102260597B (en) * | 2010-05-27 | 2013-04-24 | 中国石油化工股份有限公司 | Preparation method of high purity biodiesel |
| CN102260596B (en) * | 2010-05-27 | 2013-04-24 | 中国石油化工股份有限公司 | Method for preparing biodiesel by two-step process |
| CN103013678A (en) * | 2011-09-20 | 2013-04-03 | 中国石油化工股份有限公司 | Method for reducing biodiesel crude product acid value, and biodiesel preparation method |
| CN103013678B (en) * | 2011-09-20 | 2014-12-31 | 中国石油化工股份有限公司 | Method for reducing biodiesel crude product acid value, and biodiesel preparation method |
| CN103173281A (en) * | 2011-12-21 | 2013-06-26 | 中国石油化工股份有限公司 | Method for reducing acid value of biodiesel crude product and preparation method of biodiesel |
| CN103173281B (en) * | 2011-12-21 | 2014-12-31 | 中国石油化工股份有限公司 | Method for reducing acid value of biodiesel crude product and preparation method of biodiesel |
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| Publication number | Publication date |
|---|---|
| CN100460482C (en) | 2009-02-11 |
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