CN103242966A - Technology process for producing biodiesel and key preparation device - Google Patents
Technology process for producing biodiesel and key preparation device Download PDFInfo
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- CN103242966A CN103242966A CN2013101859183A CN201310185918A CN103242966A CN 103242966 A CN103242966 A CN 103242966A CN 2013101859183 A CN2013101859183 A CN 2013101859183A CN 201310185918 A CN201310185918 A CN 201310185918A CN 103242966 A CN103242966 A CN 103242966A
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Abstract
The invention discloses a technology process for producing biodiesel and a key preparation device. The technology process mainly comprises the following steps of: carrying out hydrolysis reaction on raw material oil and softened water so as to generate fatty acid; carrying out esterification reaction on the fatty acid separated by a cyclone hydraulic separator and methyl alcohol under a certain condition, thereby preparing coarse fatty acid methyl ester, and separating; and distilling the coarse fatty acid methyl ester by a distilling tower, and separating, thereby obtaining fatty acid methyl ester-biodiesel. The key preparation device for achieving the technology process is a reaction tower which mainly comprises a tower body, a heavy separator, a baffle plate, an overhauling port, a distributor, a gas phase methyl alcohol inlet, a material outlet, a water outlet, a heat conduction oil inlet, a heat conduction oil outlet, a heat conduction oil jacket, a material inlet, a water inlet, a safety valve, a temperature meter, a pressure meter and a gas phase methyl alcohol outlet. The technology process for producing biodiesel and the key preparation device have the characteristics of no need of catalysts, no environmental pollution, low reaction pressure and reaction temperature, less energy consumption, low investment and running costs, wide raw material application range, high yield and the like.
Description
Affiliated technical field
The invention belongs to chemical technology field, specifically a kind of technical matters of production biofuel and crucial preparation facilities.
Background technology
Growing tension along with the international energy situation, particularly carry out energetically under the background of energy-saving and emission-reduction in country, biofuel is as a kind of renewable new forms of energy, can be used as oil-fired substitute products, be subjected to the extensive concern of the whole society gradually, " biofuel " maximum characteristics are its recyclabilities, and resource is exhausted never.Biofuel can vegetables oil, animal oil is the raw material manufacturing, but many at present be raw materials for production with lipid acid, swill oil, city sewer oil, refining tankage.Discarded food oils are the animal and plant grease that can not eat again that food and drink restaurant and food processing enterprises produce in production, business process, comprise the grease of discarding after the food through repeatedly frying in shallow oil, exploding, because these waste oils all enter sewer line or oil removal in the slag sewage lagoon, therefore be commonly called as sewer oil.Along with China's food service industry and food and restaurant service industry develop rapidly, the annual discarded food oils that produce are also more and more, and " recycling " production biofuel of discarded food oils is a kind of effective ways of containment " poison oil ".Present domestic biodiesel technology respectively has characteristics, mainly contains three kinds of production technique, is respectively chemical method, supercritical methanol technology and biological enzyme.The chemical process comparative maturity, mainly contain soda acid Process, solid acid Process etc., belong to atmospheric preparation method, but need use bronsted lowry acids and bases bronsted lowry as catalyzer, exist serious environmental to pollute, influence quality product, acid-base catalysis process catalyst cost is lower, and is relatively good to the acidifying oil effect of high acid value, not good enough to the grease reaction effect of low acid value, and sulfuric acid process has certain corrosion and infringement to equipment, grease, environment, and product yield is low; The principle of solid acid technology is fallen acid value to the raw material glycerine esterification exactly, and equipment and grease are not had corrodibility, but need wash resultant methyl esters and glycerine, pickling and neutralization, so also produce the waste water that environment is caused environmental pollution, energy consumption is higher, and yield is lower, glycerin treatment cost height; Supercritical methanol technology arts demand High Temperature High Pressure, temperature of reaction 280-350 ℃, reaction pressure 4Mpa, speed of reaction is fast, transformation efficiency is high, pollution-free, adopt tubular reactor, successive reaction, the level of automation height reduces personnel selection, catalyst-free, but need initiator, to the equipment requirements height, investment and running cost height, to ingredient requirement height, poor selectivity, be suitable for fully that single vegetables oil, animal oil is the raw material manufacturing, when utilizing sewer oil to make raw material, need be to raw material processing treatment and sizing screening; Subcritical method technology, substantially with supercritical methanol technology technology, temperature, pressure reduce a little, and temperature of reaction 260-280 ℃, reaction pressure 2Mpa, catalyst-free, but long reaction time; The reaction conditions gentleness of biological process technology, adaptability to raw material is wide, non-pollutant discharge and need not washing, but its life-span for preparing used lipase is shorter usually, causes the catalytic process cost higher.
Summary of the invention
The objective of the invention is: overcome in the existing production of biodiesel Technology, need catalyzer, environmental pollution is serious, reaction pressure, temperature are higher, to the equipment requirements height, investment and running cost height, to ingredient requirement height, poor selectivity, long reaction time, energy consumption height, the shortcoming of aspects such as yield is low, providing a kind of does not need to use catalyzer, non-environmental-pollution, reaction pressure and temperature of reaction lower, less energy consumption, and investment and running cost are low, the raw material scope of application is extensive, the Technology of the production biofuel that yield is high and crucial preparation facilities.
The technical solution adopted for the present invention to solve the technical problems is: the Technology of this production biofuel, mainly finish successively as follows:
The first step is that raw oil material, softening water are added hydrolysis reaction tower by volume pump respectively, reaction under certain condition is hydrolyzed, generate lipid acid and glycerine, the mol ratio of water and grease is 4-5: 1, temperature of reaction is 170-190 ℃, reaction pressure is 1.2-1.6Mpa, and the reaction times is 2-3 hour;
Second step be through wet cyclone with lipid acid and glycerol liquor mixture separation, lipid acid enters esterification reaction tower, the glycerol liquor mixture is through concentrating generation glycerine;
The 3rd step was after the lipid acid of some amount is added esterification reaction tower, in esterification reaction tower, feed gas-phase methanol, lipid acid and methyl alcohol carry out esterification under certain condition, the mol ratio of methyl alcohol and lipid acid is 12-15: 1, temperature of reaction is 160-180 ℃, reaction pressure is 1.2-1.5Mpa, and the reaction times is 2-2.5 hour;
The 4th step utilized gas-liquid separator that methyl alcohol, water are separated with crude fatty acid methyl ester, and methyl alcohol, water enter rectifying tower as gas phase, carried out separating of methyl alcohol and water, and crude fatty acid methyl ester enters distillation tower;
The 5th step was to utilize distillation tower that crude fatty acid methyl ester is distilled, and separated obtaining fatty acid methyl ester---biofuel and plant asphalt.
The crucial preparation facilities of realizing the technical matters of production biofuel of the present invention is reaction tower, and it is mainly by tower body, heavily divide device, traverse baffle, access opening, sparger, gas-phase methanol import, discharge port, water outlet, heat conductive oil inlet, thermal oil outlet, thermal oil chuck, opening for feed, water-in, safety valve, thermometer, tensimeter, gas-phase methanol outlet to form; The outer bottom of described tower body is installed gas-phase methanol import, discharge port, water outlet respectively; The inner bottom part of described tower body is provided with sparger, and this sparger is connected with the pipeline of gas-phase methanol import; The Lower Half of described tower body is provided with thermal oil chuck, heat conductive oil inlet, thermal oil outlet, access opening; The inner top of described tower body is provided with and heavily divides device; Evenly be distributed with several traverse baffles on the interior drum wall of described tower body; The outer top of described tower body is provided with opening for feed, water-in, safety valve, thermometer, tensimeter, gas-phase methanol outlet.
The invention has the beneficial effects as follows: adopt above-mentioned Technology production biofuel, raw oil material, softening water are added hydrolysis reaction tower by volume pump respectively, reaction under certain condition is hydrolyzed, generation is easy to carry out the lipid acid of esterification, react the generation crude fatty acid methyl ester with gas-phase methanol again, carry out fractionation by distillation then and obtain fatty acid methyl ester---biofuel.
The crucial preparation facilities reaction tower of the technical matters of the production biofuel of the present invention of employing said structure, the sparger that the tower body inner bottom part arranges can upwards be distributed to the gas-phase methanol that the import through gas-phase methanol enters in the tower body in the lipid acid liquid comparatively equably; The heavily branch device that the tower body inner top is provided with can appropriate stop the discharge of gas-phase methanol; Evenly be distributed with several traverse baffles on the drum wall of tower body inside, gas-phase methanol turned back in the baffling passage of its formation advance.Thereby increase the reaction times of gas-phase methanol and lipid acid liquid, improve speed of response, increase product yield.
Compare with traditional chemical method, do not need to use catalyzer in the technological process, non-environmental-pollution does not have corrosion to equipment, good product quality, and the reaction times is short, the yield height; Compare with supercritical methanol technology, subcritical method, because increased hydrolysis reaction, desired reaction temperature, pressure have bigger reduction, speed of reaction is fast, and less energy consumption is low for equipment requirements, investment and running cost are low, and investment and running cost are low, and the raw material scope of application is extensive.
Improve as the present invention, the reaction tower that described hydrolysis reaction tower, esterification reaction tower are integrated after hydrolysis reaction generates lipid acid and glycerine, generates glycerine through concentrating after the glycerol liquor mixture isolated through wet cyclone; Feed gas-phase methanol in remaining the reaction tower that lipid acid is arranged, lipid acid and methyl alcohol carry out esterification under certain condition, are conducive to reduce investment, save cost, reduce energy consumption.
As a further improvement on the present invention, described reaction tower is some right, when wherein first reaction tower of every pair of reaction tower is hydrolyzed reaction, second reaction tower carries out esterification, first reaction tower carries out esterification then, the reaction that is hydrolyzed of second reaction tower, so alternate cycles is carried out chemical reaction.After first reaction tower hydrolysis reaction was finished, the glycerol liquor mixture of its high temperature was sent into second reaction tower by control device and is used, vice versa, thus the glycerol liquor mixture of high temperature repeatedly can be used, cut down the consumption of energy effectively, save production cost.
Improvement as the crucial preparation facilities of production biofuel of the present invention, device was provided with thrust-augmenting nozzle in described heavy minute, the upper end of this thrust-augmenting nozzle is connected heavily to be divided on the device, insert below the lipid acid liquid level lower end, be conducive to react with lipid acid heavily dividing the gas-phase methanol of collecting on the device to import in the lipid acid liquid, improve speed of response, reduce the reaction times, improve product yield.
Further improvement as the crucial preparation facilities of production biofuel of the present invention, be provided with the thermal oil coil pipe in the described tower body, the two ends of this thermal oil coil pipe are connected with the thermal oil chuck respectively, can further improve heating efficiency and uniformity coefficient, improve speed of response, reduce the reaction times, improve product yield, reduce production energy consumption.
Further improvement as the crucial preparation facilities of production biofuel of the present invention, described traverse baffle and tower body are 20-30 ° of angle, be conducive to gas-phase methanol and the lipid acid liquid mixture forms eddy flow in tower body, strengthen gas-phase methanol and lipid acid liquid mixing effect, improve speed of response, reduce the reaction times, improve product yield.
Description of drawings
Be described further below in conjunction with technical matters and the crucial preparation facilities of drawings and Examples to production biofuel of the present invention.
Fig. 1 is the process flow diagram of first embodiment of technical matters of production biofuel of the present invention;
Fig. 2 is the process flow diagram of second embodiment of technical matters of production biofuel of the present invention;
Fig. 3 is the cross-sectional view of the crucial preparation facilities embodiment of production biofuel of the present invention;
Among the figure: 1, gas-phase methanol outlet, 2, tensimeter, 3, heavily divide device, 4, thrust-augmenting nozzle, 5, thermal oil chuck, 6, the eddy flow plate, 7, access opening, 8, the gas-phase methanol import, 9, discharge port, 10, water outlet, 11, the thermal oil outlet, 12, heat conductive oil inlet, 13, thermometer, 14, safety valve, 15, thermal oil coil pipe, 16, tower body, 17, sparger, 18, opening for feed, 19, water-in, 20, the lipid acid liquid level.
Embodiment
As shown in Figure 1, the Technology of this production biofuel, mainly finish successively as follows:
The first step is that raw oil material, softening water are added hydrolysis reaction tower by volume pump respectively, reaction under certain condition is hydrolyzed, generate lipid acid and glycerine, the mol ratio of water and grease is 4-5: 1, temperature of reaction is 170-190 ℃, reaction pressure is 1.2-1.6Mpa, and the reaction times is 2-3 hour;
Second step be through wet cyclone with lipid acid and glycerol liquor mixture separation, lipid acid enters esterification reaction tower, the glycerol liquor mixture is through concentrating generation glycerine;
The 3rd step was after the lipid acid of some amount is added esterification reaction tower, in esterification reaction tower, feed gas-phase methanol, lipid acid and methyl alcohol carry out esterification under certain condition, the mol ratio of methyl alcohol and lipid acid is 12-15: 1, temperature of reaction is 160-180 ℃, reaction pressure is 1.2-1.5Mpa, and the reaction times is 2-2.5 hour;
The 4th step utilized gas-liquid separator that methyl alcohol, water are separated with crude fatty acid methyl ester, and methyl alcohol, water enter rectifying tower as gas phase, carried out separating of methyl alcohol and water, and crude fatty acid methyl ester enters distillation tower;
The 5th step was to utilize distillation tower that crude fatty acid methyl ester is distilled, and separated obtaining fatty acid methyl ester---biofuel and plant asphalt.
Adopt above-mentioned Technology production biofuel, raw oil material, softening water are added hydrolysis reaction tower by volume pump respectively, reaction under certain condition is hydrolyzed, generation is easy to carry out the lipid acid of esterification, react the generation crude fatty acid methyl ester with gas-phase methanol again, carry out fractionation by distillation then and obtain fatty acid methyl ester---biofuel.
As shown in Figure 3, the crucial preparation facilities of realizing the technical matters of production biofuel of the present invention is reaction tower, and it is mainly by tower body 16, heavily divide device 3, traverse baffle 6, access opening 7, sparger 17, gas-phase methanol import 8, discharge port 9, water outlet 10, heat conductive oil inlet 11, thermal oil outlet 12, thermal oil chuck 5, opening for feed 18, water-in 19, safety valve 14, thermometer 13, tensimeter 2, gas-phase methanol outlet 1 to form; The outer bottom of described tower body 16 is installed gas-phase methanol import 8, discharge port 9, water outlet 10 respectively; The inner bottom part of described tower body 16 is provided with sparger 17, and this sparger 17 is connected with the pipeline of gas-phase methanol import 8; The Lower Half of described tower body 16 is provided with thermal oil chuck 5, heat conductive oil inlet 11, thermal oil outlet 12, access opening 7; The inner top of described tower body 16 is provided with and heavily divides device 3; Evenly be distributed with several traverse baffles 6 on the interior drum wall of described tower body 16; The outer top of described tower body 16 is provided with opening for feed 18, water-in 19, safety valve 14, thermometer 13, tensimeter 2, gas-phase methanol outlet 1.
The crucial preparation facilities reaction tower of the technical matters of the production biofuel of the present invention of employing said structure, the sparger 17 that tower body 16 inner bottom parts arrange can upwards be distributed to the gas-phase methanol that enters in the tower body 16 through gas-phase methanol import 8 in the lipid acid liquid comparatively equably; The heavily branch device 3 that tower body 16 inner tops are provided with can appropriate stop the discharge of gas-phase methanol; Evenly be distributed with several traverse baffles 6 on the drum wall of tower body 16 inside, gas-phase methanol turned back in the baffling passage of its formation advance.Thereby increase the reaction times of gas-phase methanol and lipid acid liquid, improve speed of response, increase product yield.
Compare with traditional chemical method, do not need to use catalyzer in the technological process, non-environmental-pollution does not have corrosion to equipment, good product quality, and the reaction times is short, the yield height; Compare with supercritical methanol technology, subcritical method, because increased hydrolysis reaction, desired reaction temperature, pressure have bigger reduction, speed of reaction is fast, and less energy consumption is low for equipment requirements, investment and running cost are low, and investment and running cost are low, and the raw material scope of application is extensive.
As shown in Figure 2, improve as the present invention, the reaction tower that described hydrolysis reaction tower, esterification reaction tower are integrated after hydrolysis reaction generates lipid acid and glycerine, generates glycerine through concentrating after the glycerol liquor mixture isolated through wet cyclone; Feed gas-phase methanol in remaining the reaction tower that lipid acid is arranged, lipid acid and methyl alcohol carry out esterification under certain condition, are conducive to reduce investment, save cost, reduce energy consumption.
As a further improvement on the present invention, described reaction tower is some right, when wherein first reaction tower of every pair of reaction tower is hydrolyzed reaction, second reaction tower carries out esterification, first reaction tower carries out esterification then, the reaction that is hydrolyzed of second reaction tower, so alternate cycles is carried out chemical reaction.After first reaction tower hydrolysis reaction was finished, the glycerol liquor mixture of its high temperature was sent into second reaction tower by control device and is used, vice versa, thus the glycerol liquor mixture of high temperature repeatedly can be used, cut down the consumption of energy effectively, save production cost.
As shown in Figure 3, improvement as the crucial preparation facilities of production biofuel of the present invention, device 3 was provided with thrust-augmenting nozzle 4 in described heavy minute, the upper end of this thrust-augmenting nozzle 4 is connected heavily to be divided on the device 3, and the lipid acid liquid level is inserted below 20 in the lower end, is conducive to heavily dividing the gas-phase methanol of collecting on the device 3 to import in the lipid acid liquid, react with lipid acid, improve speed of response, reduce the reaction times, improve product yield.
As shown in Figure 3, further improvement as the crucial preparation facilities of production biofuel of the present invention, be provided with thermal oil coil pipe 15 in the described tower body 16, the two ends of this thermal oil coil pipe 15 are connected with thermal oil chuck 5 respectively, can further improve heating efficiency and uniformity coefficient, improve speed of response, reduce the reaction times, improve product yield, reduce production energy consumption.
As shown in Figure 3, further improvement as the crucial preparation facilities of production biofuel of the present invention, described traverse baffle 6 is 20-30 ° of angle with tower body 16, be conducive to gas-phase methanol and lipid acid liquid mixture and in tower body 16, form eddy flow, strengthen gas-phase methanol and lipid acid liquid mixing effect, improve speed of response, reduce the reaction times, improve product yield.
Claims (9)
1. technical matters of producing biofuel is characterized in that this technical matters finishes as follows successively:
The first step is that raw oil material, softening water are added hydrolysis reaction tower by volume pump respectively, reaction under certain condition is hydrolyzed, generate lipid acid and glycerine, the mol ratio of water and grease is 4-5: 1, temperature of reaction is 170-190 ℃, reaction pressure is 1.2-1.6Mpa, and the reaction times is 2-3 hour;
Second step be through wet cyclone with lipid acid and glycerol liquor mixture separation, lipid acid enters esterification reaction tower, the glycerol liquor mixture is through concentrating generation glycerine;
The 3rd step was after the lipid acid of some amount is added esterification reaction tower, in esterification reaction tower, feed gas-phase methanol, lipid acid and methyl alcohol carry out esterification under certain condition, the mol ratio of methyl alcohol and lipid acid is 12-15: 1, temperature of reaction is 160-180 ℃, reaction pressure is 1.2-1.5Mpa, and the reaction times is 2-2.5 hour;
The 4th step utilized gas-liquid separator that methyl alcohol, water are separated with crude fatty acid methyl ester, and methyl alcohol, water enter rectifying tower as gas phase, carried out separating of methyl alcohol and water, and crude fatty acid methyl ester enters distillation tower;
The 5th step was to utilize distillation tower that crude fatty acid methyl ester is distilled, and separated obtaining fatty acid methyl ester---biofuel and plant asphalt.
2. the technical matters of production biofuel according to claim 1, it is characterized in that: the reaction tower that described hydrolysis reaction tower, esterification reaction tower are integrated, after hydrolysis reaction generates lipid acid and glycerine, generate glycerine through concentrating after the glycerol liquor mixture isolated through wet cyclone; Feed gas-phase methanol in remaining the reaction tower that lipid acid is arranged, lipid acid and methyl alcohol carry out esterification under certain condition.
3. the technical matters of production biofuel according to claim 2, it is characterized in that: described reaction tower is some right, when wherein first reaction tower of every pair of reaction tower is hydrolyzed reaction, second reaction tower carries out esterification, first reaction tower carries out esterification then, the reaction that is hydrolyzed of second reaction tower, so alternate cycles is carried out chemical reaction.
4. realize the crucial preparation facilities of the technical matters of described any one the production biofuel of claim 1 to 3, it is characterized in that: described reaction tower is by tower body (16), heavily divide device (3), traverse baffle (6), access opening (7), sparger (17), gas-phase methanol import (8), discharge port (9), water outlet (10), heat conductive oil inlet (11), thermal oil outlet (12), thermal oil chuck (5), opening for feed (18), water-in (19), safety valve (14), thermometer (13), tensimeter (2), gas-phase methanol outlet (1) to form; The outer bottom of described tower body (16) is installed gas-phase methanol import (8), discharge port (9), water outlet (10) respectively; The inner bottom part of described tower body (16) is provided with sparger (17), and this sparger (17) is connected with the pipeline of gas-phase methanol import (8); The Lower Half of described tower body (16) is provided with thermal oil chuck (5), heat conductive oil inlet (11), thermal oil outlet (12), access opening (7); The inner top of described tower body (16) is provided with and heavily divides device (3); Evenly be distributed with several traverse baffles (6) on the interior drum wall of described tower body (16); The outer top of described tower body (16) is provided with opening for feed (18), water-in (19), safety valve (14), thermometer (13), tensimeter (2), gas-phase methanol outlet (1).
5. the crucial preparation facilities of production biofuel according to claim 4, it is characterized in that: described heavy minute device (3) be provided with some thrust-augmenting nozzles (4), the upper end of this thrust-augmenting nozzle (4) is connected heavily divides device (on 3), and insert below the lipid acid liquid level (20) lower end.
6. the crucial preparation facilities of production biofuel according to claim 4, it is characterized in that: be provided with thermal oil coil pipe (15) in the described tower body (16), the two ends of this thermal oil coil pipe (15) are connected with thermal oil chuck (5) respectively.
7. the crucial preparation facilities of production biofuel according to claim 5, it is characterized in that: be provided with thermal oil coil pipe (15) in the described tower body (16), the two ends of this thermal oil coil pipe (15) are connected with thermal oil chuck (5) respectively.
8. the crucial preparation facilities of production biofuel according to claim 4 is characterized in that: described traverse baffle (6) is 20-30 ° of angle with tower body (16).
9. according to the crucial preparation facilities of any one described production biofuel of claim 4 to 6, it is characterized in that: described traverse baffle (6) is 20-30 ° of angle with tower body (16).
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103468413A (en) * | 2013-09-25 | 2013-12-25 | 陕西合盛生物柴油技术开发有限公司 | Production method of biodiesel |
| CN104673502A (en) * | 2015-02-03 | 2015-06-03 | 江苏西方环保科技有限公司 | Continuous esterification technique for producing biodiesel from waste grease |
| CN105316114A (en) * | 2014-06-25 | 2016-02-10 | 金广恒环保技术（南京）有限公司 | Recycle utilization system of converting drainage oil into bio-diesel |
| CN106190591A (en) * | 2015-08-27 | 2016-12-07 | 上海中器环保科技有限公司 | The esterification of a kind of biodiesel, ester exchange reaction method |
| CN108192740A (en) * | 2018-03-22 | 2018-06-22 | 淮阴师范学院 | The synthesis technology and equipment of a kind of biodiesel |
| CN108373947A (en) * | 2018-04-08 | 2018-08-07 | 淮阴师范学院 | A kind of process units and preparation method of composite biodiesel |
| CN109593570A (en) * | 2018-12-11 | 2019-04-09 | 天津大学 | A method of biodiesel is prepared using wet microalgae two-step reaction |
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| CN202186999U (en) * | 2011-08-03 | 2012-04-11 | 龙岩卓越新能源发展有限公司 | Crude biodiesel flash tower |
| CN202530065U (en) * | 2012-04-27 | 2012-11-14 | 陕西德融科技信息发展有限公司 | Special reaction kettle for producing biodiesel by using high-acid-value oil |
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| CN202186999U (en) * | 2011-08-03 | 2012-04-11 | 龙岩卓越新能源发展有限公司 | Crude biodiesel flash tower |
| CN202530065U (en) * | 2012-04-27 | 2012-11-14 | 陕西德融科技信息发展有限公司 | Special reaction kettle for producing biodiesel by using high-acid-value oil |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103468413A (en) * | 2013-09-25 | 2013-12-25 | 陕西合盛生物柴油技术开发有限公司 | Production method of biodiesel |
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| CN105316114A (en) * | 2014-06-25 | 2016-02-10 | 金广恒环保技术（南京）有限公司 | Recycle utilization system of converting drainage oil into bio-diesel |
| CN104673502A (en) * | 2015-02-03 | 2015-06-03 | 江苏西方环保科技有限公司 | Continuous esterification technique for producing biodiesel from waste grease |
| CN106190591A (en) * | 2015-08-27 | 2016-12-07 | 上海中器环保科技有限公司 | The esterification of a kind of biodiesel, ester exchange reaction method |
| CN108192740A (en) * | 2018-03-22 | 2018-06-22 | 淮阴师范学院 | The synthesis technology and equipment of a kind of biodiesel |
| CN108373947A (en) * | 2018-04-08 | 2018-08-07 | 淮阴师范学院 | A kind of process units and preparation method of composite biodiesel |
| CN109593570A (en) * | 2018-12-11 | 2019-04-09 | 天津大学 | A method of biodiesel is prepared using wet microalgae two-step reaction |
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Application publication date: 20130814 |