CN101173176A - Technique for continuous production of biological diesel oil with propagation waste oil - Google Patents
Technique for continuous production of biological diesel oil with propagation waste oil Download PDFInfo
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- CN101173176A CN101173176A CNA2007100123887A CN200710012388A CN101173176A CN 101173176 A CN101173176 A CN 101173176A CN A2007100123887 A CNA2007100123887 A CN A2007100123887A CN 200710012388 A CN200710012388 A CN 200710012388A CN 101173176 A CN101173176 A CN 101173176A
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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 provides a technological method that utilizes the waste oil of animals and plants to continuously produce biodiesel. The technical proposal of the invention is that, waste edible oil, high acid value oil, animal and vegetable oils, oil foot and other components are used as materials; dehydration treatment, esterification and transesterification, methanol recovery, separation of fatty acid methyl ester and glycerol according to densities by a centrifuge, molecule distillation deacidification, high temperature decomposition of ester soluble impurity, and molecule distillation deodorization are directly performed; the finished product, which is light yellow fatty acid methyl ester, namely 0<#> biodiesel, is acquired by continuous production. The method continuously and rapidly semi-automatically completes esterification and transesterification reaction to get fatty acid methyl ester under completely vacuum condition at a certain temperature, and the problems of high production cost, low yield and long reaction time of biodiesel production by common esterification method are effectively solved. The invention has the advantages of no three wastes produced during the whole production process, green environmental protection, obviously lowered labor intensity, easy operation, low energy consumption, effectively reduced production cost of the biodiesel, fast reaction rate, improved productivity, and fitness for large scale industrial production.
Description
Technical field
The present invention relates to a kind of processing method of utilizing propagation waste oil continuous production biofuel.It is to utilize waste edible oil, high acid value oil, vegetable and animals oils, oil foot etc. directly to carry out processed, esterification transesterify, Methanol Recovery, whizzer by density separation fatty acid methyl ester (biofuel) and glycerine, molecular distillation depickling, elevated temperature heat decomposition ester solubility impurity, molecular distillation deodorization for raw material, and continuous production gets finished product fatty acid methyl ester (promptly 0
#Biofuel) technical process.
Background technology
Along with the progress of society, the reach of science, human living space to self requires more and more higher.The Pollution abatement of atmosphere and water has been mentioned routine work as the course that must solve.The Eleventh Five-Year Plan period, country saves oil by implementing to implement the motor vehicle fuel economy standard and the measures such as policy and system that match with clean coal, refinery coke, substitute gas oil fuel; Implement the cleaning vehicle action plan, the development hybrid vehicle is promoted gas combustion automobile, the popularization of quickening Aalcohols fuel and coal liquefaction engineering construction progress, development alternative fuel at urban bus, taxi etc.Diesel oil occupies higher share as a kind of important refining of petroleum product in various countries' fuel structure, to become important power fuel.Quickening along with vehicle diesel oil trend in the world wide, the demand of following diesel oil can be more and more big, and the raising of exhausted day by day and people's environmental consciousness of petroleum resources, promoted countries in the world to accelerate the exploitation paces of diesel oil alternative fuel greatly, especially entered the nineties in 20th century, biofuel can be easy to reach diesel oil II, the requirement of III class standard of " world's fuel oil standard " with its excellent environmental-protecting performance, more and more is subjected to the attention of various countries.The technology of existing production of biodiesel do not realize in dehydration or biodiesel raw material pre-treatment and esterification transesterify process the monitoring in the reaction process, thus complex process waste raw material, the energy consumption height, the cost height, yield rate is low; Simultaneously impurity such as biofuel and glycerine separate with purification process in what use is washing process, the waste water,waste gas and industrial residue discharging is arranged.Therefore existing manufacturing technique is badly in need of improving.
China is one of the country the most rapidly of Economic development in the world, demand to the energy grows continuously and fast for a long time, in present energy consumption constitutes, except that coal can satisfy the self-sufficiency, oil every year need be from a large amount of imports on the world market, so not only increase the drain of foreign exchange of buying oil, and caused the negative impact that can not be ignored for the steady progression of China's economy.
Summary of the invention
The purpose of this invention is to provide a kind of processing method of utilizing propagation waste oil continuous production biofuel.It can effectively solve with common esterification method and apparatus production production of biodiesel cost height, yield rate is low, problems such as long reaction time, no three wastes problem in the production process, environmental protection, production technique serialization, technology height reduce labour intensity, improve yield, operation and energy consumption are low easily, reduce production costs, boost productivity, be fit to large-scale industrial production.
The processing method that provides of the present invention is as follows:
1) biodiesel raw material sucks the continous vacuum esterifying kettle automatically under vacuum state;
2) by heat conducting oil boiler the continous vacuum esterifying kettle is heated, at true temp is 50-70 ℃, vacuum tightness is-0.075～-the 0.095Mpa condition under, biodiesel raw material is distilled the condensation dehydration, by online moisture measurement meter monitoring, moisture content is reduced in 1%;
3) under vacuum condition, in raw materials quality ratio 20-30%, concentration is that 99% methyl alcohol and an acidic catalyst of 1-1.2% enter the continous vacuum esterifying kettle that is equipped with through the biodiesel raw material of processed, temperature be 40-50 ℃ and vacuum tightness be-0.075～-carry out the esterification transesterification reaction under the 0.095Mpa condition, reaction times is 20-40 minute, by online PH acidity measurement meter monitoring pH value, pH value 1-6;
4) be 50-70 ℃ at true temp, vacuum tightness is-0.075～-remaining methyl alcohol and portion water azeotropic condense to the Methanol Recovery hold-up vessel in will reacting under the 0.095Mpa condition; The methanol solution that reclaims carries out methanol rectification by methanol rectifying tower, purity is that 99% methyl alcohol utilizes once more;
5) crude fatty acid methyl ester after reaction finishes and the mixture of glycerine enter into surge tank, under 80 ℃ condition, by the butterfly centrifugal separating machine glycerine are separated with crude fatty acid methyl ester;
6) temperature is at 70-120 ℃, and vacuum tightness is under the condition of 1pa-20pa, and crude fatty acid methyl ester is by the depickling of one-level scraped film type molecular distillation tower, and acid number directly drops in 0.3%;
7) fatty acid methyl ester after the depickling enters in the elevated temperature heat decomposition pot, carries out thermolysis 10-15 minute under the condition of normal pressure of 260 ℃-280 ℃ of temperature, is cooled to 130-140 ℃ then;
8) fatty acid methyl ester after the thermolysis is in secondary scraped film type molecular distillation tower, and at 140-200 ℃, vacuum tightness is to carry out further rectifying deodorization under the condition of 1pa-20pa, and the lipoid in the fatty acid methyl ester are taken off, and obtains meeting 0 of national standard
#Biofuel.
The used raw material of the present invention is waste edible oil, high acid value oil, vegetable and animals oils, vegetables oil oil foot.
The present invention has following advantage compared with the prior art: it has effectively solved with common esterification method and apparatus production production of biodiesel cost height, yield rate is low, problems such as long reaction time, particularly whole process of production does not have the three wastes (waste water, waste gas, waste residue) produces, environmental protection, production technique has serialization, the high characteristics of technology, significantly reduce labour intensity, the method of free acid is that the alkali refining method not only makes a large amount of saponification of tri-glyceride in the tri-glyceride to efficiently solve traditional removing, influence yield, and make product be subjected to the pollution problems of chemical; Operation and energy consumption are low easily, effectively reduce the production of biodiesel cost, and speed of response is fast, has improved productivity, are fit to large-scale industrial production.
Description of drawings
Fig. 1 is a process flow diagram of the present invention.
Embodiment
The used biodiesel raw material of the present invention is waste edible oil, high acid value oil, vegetable and animals oils, oil foot.
1) biodiesel raw material sucks the continous vacuum esterifying kettle automatically under vacuum state;
2) by heat conducting oil boiler the continous vacuum esterifying kettle is heated, at true temp is 50-70 ℃, vacuum tightness is-0.075～-the 0.095Mpa condition under, biodiesel raw material is distilled the condensation dehydration, by online moisture measurement meter monitoring, moisture content is reduced in 1%;
3) under vacuum condition, in raw materials quality ratio 20-30%, concentration is that 99% methyl alcohol and an acidic catalyst of 1-1.2% enter the continous vacuum esterifying kettle that is equipped with through the biodiesel raw material of processed, an acidic catalyst can be selected the vitriol oil more than 98% for use, temperature be 40-50 ℃ and vacuum tightness be-0.075～-carry out the esterification transesterification reaction under the 0.095Mpa condition, reaction times is 20-40 minute, by online PH acidity measurement meter monitoring pH value, pH value 1-6;
4) be 50-70 ℃ at true temp, vacuum tightness is-0.075～-remaining methyl alcohol and portion water azeotropic condense to the Methanol Recovery hold-up vessel in will reacting under the 0.095Mpa condition; The methanol solution that reclaims carries out methanol rectification by methanol rectifying tower, purity is that 99% methyl alcohol utilizes once more;
5) crude fatty acid methyl ester after reaction finishes and the mixture of glycerine enter into surge tank, under 80-90 ℃ condition, by the butterfly centrifugal separating machine glycerine are separated with crude fatty acid methyl ester;
6) crude fatty acid methyl ester is heated to 100 ℃, delivers to one-level scraped film type molecular distillation tower.Crude fatty acid methyl ester is by the depickling of one-level scraped film type molecular distillation tower, and temperature is at 70-120 ℃, and vacuum tightness is under the condition of 1pa-20pa, and acid number directly drops in 0.3%;
7) fatty acid methyl ester after the depickling enters in the elevated temperature heat decomposition pot, carries out thermolysis 10-15 minute under 260 ℃-280 ℃ condition of normal pressure, is cooled to 130-140 ℃ then;
8) fatty acid methyl ester after the thermolysis is in secondary scraped film type molecular distillation tower, and at 140-200 ℃, vacuum tightness is to carry out further rectifying deodorization under the condition of 1pa-20pa, and the lipoid in the fatty acid methyl ester are taken off, and obtains meeting 0 of national standard
#Biofuel.
The equipment that the present invention adopts is existing known equipment.
Gained biofuel transformation efficiency of the present invention is more than 95%, reclaims methanol purity more than 99%.
Its main technical process as shown in Figure 1.
Claims (3)
1. processing method of utilizing propagation waste oil continuous production biofuel is characterized in that:
1) biodiesel raw material sucks the continous vacuum esterifying kettle automatically under vacuum state;
2) by heat conducting oil boiler the continous vacuum esterifying kettle is heated, at true temp is 50-70 ℃, vacuum tightness is-0.075～-the 0.095Mpa condition under, biodiesel raw material is distilled the condensation dehydration, by online moisture measurement meter monitoring, moisture content is reduced in 1%;
3) under vacuum condition, in raw materials quality ratio 20-30%, concentration is that 99% methyl alcohol and an acidic catalyst of 1-1.2% enter the continous vacuum esterifying kettle that is equipped with through the biodiesel raw material of processed, temperature be 40-50 ℃ and vacuum tightness be-0.075～-carry out the esterification transesterification reaction under the 0.095Mpa condition, reaction times is 2040 minutes, by online PH acidity measurement meter monitoring pH value, pH value 1-6;
4) be 50-70 ℃ at true temp, vacuum tightness is-0.075～-remaining methyl alcohol and portion water azeotropic condense to the Methanol Recovery hold-up vessel in will reacting under the 0.095Mpa condition; The methanol solution that reclaims carries out methanol rectification by methanol rectifying tower, purity is that 99% methyl alcohol utilizes once more;
5) crude fatty acid methyl ester after reaction finishes and the mixture of glycerine enter into surge tank, under 80 ℃ condition, by the butterfly centrifugal separating machine glycerine are separated with crude fatty acid methyl ester;
6) temperature is at 70-120 ℃, and vacuum tightness is under the condition of 1pa-20pa, and crude fatty acid methyl ester is by the depickling of one-level scraped film type molecular distillation tower, and acid number directly drops in 0.3%;
7) fatty acid methyl ester after the depickling enters in the elevated temperature heat decomposition pot, carries out thermolysis 10-15 minute under the condition of normal pressure of 260 ℃-280 ℃ of temperature, is cooled to 130-140 ℃ then;
8) fatty acid methyl ester after the thermolysis is in secondary scraped film type molecular distillation tower, at 140-200 ℃, vacuum tightness is to carry out further rectifying deodorization under the condition of 1pa-20pa, and the lipoid in the fatty acid methyl ester are taken off, and obtains meeting the 0# biofuel of national standard.
2. the processing method of utilizing propagation waste oil continuous production biofuel according to claim 1 is characterized in that: crude fatty acid methyl ester is heated 100 ℃ before entering the depickling of one-level scraped film type molecular distillation tower.
3. the processing method of utilizing propagation waste oil continuous production biofuel according to claim 1 is characterized in that: raw material is waste edible oil, high acid value oil, vegetable and animals oils, oil foot.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CNA2007100123887A CN101173176A (en) | 2007-08-07 | 2007-08-07 | Technique for continuous production of biological diesel oil with propagation waste oil |
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| CNA2007100123887A CN101173176A (en) | 2007-08-07 | 2007-08-07 | Technique for continuous production of biological diesel oil with propagation waste oil |
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| CN101173176A true CN101173176A (en) | 2008-05-07 |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102041177B (en) * | 2009-10-18 | 2013-01-16 | 陕西春光生物能源开发有限公司 | Method for preparing biodiesel |
| CN103060097A (en) * | 2012-12-30 | 2013-04-24 | 上海油好同盟新能源科技有限公司 | Continuous production line for producing biodiesel under catalysis of solid catalyst |
| CN103159590A (en) * | 2013-04-03 | 2013-06-19 | 陕西德融新能源股份有限公司 | Process for recycling excessive methyl alcohol in biodiesel production process |
| 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 |
| CN103468400A (en) * | 2013-09-25 | 2013-12-25 | 陕西合盛生物柴油技术开发有限公司 | Distillation and deodorization method for production of biodiesel |
| CN103502410A (en) * | 2011-04-14 | 2014-01-08 | 阿尔法拉瓦尔股份有限公司 | A process for autocatalytic esterification of fatty acids |
| CN104341299A (en) * | 2013-07-29 | 2015-02-11 | 漳州金富顺生物科技有限公司 | Esterification of deodorized fatty acid |
-
2007
- 2007-08-07 CN CNA2007100123887A patent/CN101173176A/en active Pending
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102041177B (en) * | 2009-10-18 | 2013-01-16 | 陕西春光生物能源开发有限公司 | Method for preparing biodiesel |
| CN103502410A (en) * | 2011-04-14 | 2014-01-08 | 阿尔法拉瓦尔股份有限公司 | A process for autocatalytic esterification of fatty acids |
| US9085547B2 (en) | 2011-04-14 | 2015-07-21 | Alfa Laval Corporate Ab | Process for autocatalytic esterification of fatty acids |
| 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 |
| CN103060097A (en) * | 2012-12-30 | 2013-04-24 | 上海油好同盟新能源科技有限公司 | Continuous production line for producing biodiesel under catalysis of solid catalyst |
| CN103060097B (en) * | 2012-12-30 | 2014-11-26 | 上海油好同盟新能源科技有限公司 | Continuous production line for producing biodiesel under catalysis of solid catalyst |
| CN103159590A (en) * | 2013-04-03 | 2013-06-19 | 陕西德融新能源股份有限公司 | Process for recycling excessive methyl alcohol in biodiesel production process |
| CN104341299A (en) * | 2013-07-29 | 2015-02-11 | 漳州金富顺生物科技有限公司 | Esterification of deodorized fatty acid |
| CN104341299B (en) * | 2013-07-29 | 2016-08-24 | 漳州金富顺生物科技有限公司 | A kind of esterification of deodorised fat acid |
| CN103468400A (en) * | 2013-09-25 | 2013-12-25 | 陕西合盛生物柴油技术开发有限公司 | Distillation and deodorization method for production of biodiesel |
| CN103468400B (en) * | 2013-09-25 | 2015-04-08 | 陕西合盛生物柴油技术开发有限公司 | Distillation and deodorization method for production of biodiesel |
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Open date: 20080507 |