CN111234933A - Device for producing biodiesel by continuous ester exchange of waste oil and fat - Google Patents
Device for producing biodiesel by continuous ester exchange of waste oil and fat Download PDFInfo
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- CN111234933A CN111234933A CN202010206971.7A CN202010206971A CN111234933A CN 111234933 A CN111234933 A CN 111234933A CN 202010206971 A CN202010206971 A CN 202010206971A CN 111234933 A CN111234933 A CN 111234933A
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- Prior art keywords
- kettle
- reaction kettle
- precipitation
- reaction
- catalyst
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- 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.)
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- 239000003225 biodiesel Substances 0.000 title claims abstract description 31
- 239000002699 waste material Substances 0.000 title claims abstract description 25
- 125000004185 ester group Chemical group 0.000 title claims abstract description 14
- 238000006243 chemical reaction Methods 0.000 claims abstract description 123
- 238000001556 precipitation Methods 0.000 claims abstract description 64
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims abstract description 58
- 239000003054 catalyst Substances 0.000 claims abstract description 32
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 30
- 235000011187 glycerol Nutrition 0.000 claims abstract description 24
- 239000000463 material Substances 0.000 claims abstract description 21
- 238000003756 stirring Methods 0.000 claims abstract description 11
- 230000009286 beneficial effect Effects 0.000 claims abstract description 10
- 238000010438 heat treatment Methods 0.000 claims abstract description 9
- 238000000926 separation method Methods 0.000 claims abstract description 6
- 238000005259 measurement Methods 0.000 claims abstract description 4
- 230000002349 favourable effect Effects 0.000 claims description 3
- 238000007086 side reaction Methods 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 238000005192 partition Methods 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 18
- 239000007788 liquid Substances 0.000 description 7
- 238000000034 method Methods 0.000 description 5
- 239000003925 fat Substances 0.000 description 4
- 238000005809 transesterification reaction Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000007599 discharging Methods 0.000 description 2
- 238000005886 esterification reaction Methods 0.000 description 2
- 235000021588 free fatty acids Nutrition 0.000 description 2
- 125000005456 glyceride group Chemical group 0.000 description 2
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 235000014593 oils and fats Nutrition 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
- C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
- C11C3/04—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fats or fatty oils
- C11C3/10—Ester interchange
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/10—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by stirrers or by rotary drums or rotary receptacles or endless belts
-
- 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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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Liquid Carbonaceous Fuels (AREA)
Abstract
The invention discloses a device for producing biodiesel by continuous ester exchange of waste oil, which comprises a 1# reaction kettle, a 1# precipitation kettle, a 2# reaction kettle and a 2# precipitation kettle which are sequentially connected by pipelines; the No. 1 reaction kettle is provided with a waste oil inlet, a catalyst inlet and a methanol inlet; catalyst feeding distribution discs, heating coils, stirring devices and temperature measuring ports are arranged in the two reaction kettles, and material passing ports are arranged at the bottoms of the two reaction kettles; the bottoms of the two settling kettles are both provided with a densimeter for automatic measurement and a glycerin outlet; the No. 2 reaction kettle is provided with a catalyst replenishing feed inlet; the side surface of the upper part of the 2# precipitation kettle is provided with a feed inlet which is connected with a feed passing port pipeline of the 2# reaction kettle, the other side surface of the 2# precipitation kettle is provided with a biodiesel outlet, and the middle upper part in the kettle is provided with a middle partition plate, so that the materials flow in a U shape in the 2# precipitation kettle to be beneficial to the separation and discharge of glycerol and biodiesel. The invention has the characteristics of low investment, high automation level, good product quality and stability, low production cost and high conversion rate.
Description
Technical Field
The invention relates to production equipment for producing biodiesel by using waste oil, in particular to a device for producing biodiesel by continuous ester exchange of waste oil.
Background
The domestic biodiesel production mainly takes waste oil as a raw material, and the waste oil is a mixture mainly composed of free fatty acid and glyceride besides impurities such as water, silt and the like. After the waste oil is purified, free fatty acid is generally converted into biodiesel and water by an esterification reaction, and after the water generated by the reaction is separated, glyceride is converted into biodiesel and glycerol by an ester exchange reaction. The device for producing biodiesel by ester exchange mainly comprises a reaction kettle and a reaction tower, and has the following problems: the reaction kettle method is used for producing biodiesel intermittently, and has the problems of high labor intensity, unstable quality and the like; the reaction tower method uses high-temperature and high-pressure equipment, and has large investment, high energy consumption and high operation requirement.
Disclosure of Invention
The invention aims to provide a device for producing biodiesel by continuously performing ester exchange on waste oil and fat, which has the advantages of low investment, high automation level, good product quality and stability, low production cost and high conversion rate.
In order to realize the purpose, the device for producing the biodiesel by the continuous ester exchange of the waste oil comprises a 1# reaction kettle, a 1# precipitation kettle, a 2# reaction kettle, a 2# precipitation kettle and a connecting pipeline; the top of the No. 1 reaction kettle is provided with a waste oil inlet a, a No. 1 reaction kettle methanol inlet b and a No. 1 reaction kettle catalyst inlet c, the side surface of the No. 1 reaction kettle is provided with a No. 1 reaction kettle steam inlet g, a No. 1 reaction kettle steam condensate outlet d and a No. 1 reaction kettle temperature measuring port f, and the bottom of the No. 1 reaction kettle is provided with a No. 1 reaction kettle material passing port e; the reactor is internally provided with a catalyst feeding distribution disc, a heating coil and a stirring device, the catalyst distribution disc is beneficial to uniformly adding a catalyst into the reaction kettle so as to reduce the occurrence of side reactions, the heating coil is used for adjusting the temperature in the 1# reaction kettle to be in accordance with a set value by introducing steam so as to ensure that the ester exchange reaction is smoothly carried out, and the stirring device is beneficial to fully reacting waste oil and methanol under the action of the catalyst; the side surface of the upper part of the 1# precipitation kettle is provided with a 1# precipitation kettle feed port h which is connected with a 1# reaction kettle feed port e through a pipeline, the bottom of the 1# precipitation kettle is provided with an automatic measurement densimeter and a 1# precipitation kettle glycerol outlet i, and the side surface of the bottom of the 1# precipitation kettle is provided with a 1# precipitation kettle feed port j; the side surface of the upper part of the 2# reaction kettle is provided with a 2# reaction kettle feed port l which is connected with a 1# precipitation kettle feed port j through a pipeline, the top of the 2# reaction kettle is provided with a 2# reaction kettle catalyst feed port k, the bottom of the 2# reaction kettle is provided with a 2# reaction kettle feed port n, the side surface of the 2# reaction kettle is provided with a 2# reaction kettle steam inlet p, a 2# reaction kettle steam condensate outlet m and a 2# reaction kettle temperature measuring port o, and the kettle is internally provided with a catalyst feed distribution disc, a steam coil; 2# reation kettle's upper portion side is equipped with 2# precipitation cauldron feed inlet q and 2# reation kettle material passing hole n pipe connection, and another side is equipped with biodiesel export s, and automatic measuring densimeter is equipped with to the bottom and 2# precipitation cauldron glycerine export r is equipped with, and upper middle portion is equipped with intermediate bottom in the cauldron, makes the material be the U type in 2# precipitation cauldron and flows, is favorable to glycerine and biodiesel separation and discharge.
The device for producing biodiesel by continuous transesterification of waste oil and fat has the following technical characteristics and beneficial effects:
① realizes continuous feeding and discharging, is beneficial to automatic control, has high production efficiency, and ensures the stability of production quality;
② compared with batch method, the method has the advantages of simple operation and low labor intensity, and compared with high-temperature high-pressure reaction tower, the method has the advantage of low cost;
③ the glycerol is discharged continuously and automatically in the production process, which is beneficial to generating the biodiesel and improving the conversion rate of the ester exchange reaction.
④ has less investment and low maintenance cost.
Drawings
FIG. 1 is a schematic structural diagram of a device for producing biodiesel by continuous transesterification of waste oil and fat.
FIG. 2 is an enlarged schematic view of the reaction vessel No. 1 in FIG. 1.
FIG. 3 is an enlarged schematic view of the 1# precipitation tank in FIG. 1.
FIG. 4 is an enlarged schematic view of the 2# reaction vessel in FIG. 1.
FIG. 5 is an enlarged schematic view of the 2# precipitation tank in FIG. 1.
Reference numerals: 1 # reaction kettle 1, 1# precipitation kettle 2, 2 # reaction kettle 3, 2# precipitation kettle 4, densimeter 5, intermediate bottom 6, waste oil inlet a, 1# reaction kettle methanol inlet b, 1# reaction kettle catalyst inlet c, 1# reaction kettle steam condensate outlet d, 1# reaction kettle material passing port e, 1# reaction kettle temperature measuring port f, 1# reaction kettle steam inlet g, 1# precipitation kettle material inlet h, 1# precipitation kettle glycerin outlet i, 1# precipitation kettle material passing port j, 2# reaction kettle catalyst inlet k, 2# reaction kettle material inlet l, 2# reaction kettle steam condensate outlet m, 2# reaction kettle material outlet n, 2# reaction kettle temperature measuring port o, 2# reaction kettle steam inlet p, 2# precipitation kettle material inlet q, 2# precipitation kettle glycerin outlet r and 2# precipitation kettle material outlet s.
Detailed Description
The following describes the apparatus for producing biodiesel by continuous transesterification of waste oils and fats according to the present invention in further detail with reference to the accompanying drawings and the following embodiments.
As shown in the drawings 1-5, the device for producing biodiesel by continuous transesterification of waste oil comprises a # 1 reaction kettle 1, a # 1 precipitation kettle 2, a # 2 reaction kettle 3, a # 2 precipitation kettle 4 and a connecting pipeline; the top of the No. 1 reaction kettle 1 is provided with a waste oil inlet a, a No. 1 reaction kettle methanol inlet b and a No. 1 reaction kettle catalyst inlet c, the side surface is provided with a No. 1 reaction kettle steam inlet g, a No. 1 reaction kettle steam condensate outlet d and a No. 1 reaction kettle temperature measuring port f, and the bottom is provided with a No. 1 reaction kettle material passing port e; the reactor is internally provided with a catalyst feeding distribution disc, a heating coil and a stirring device, the catalyst distribution disc is beneficial to uniformly adding a catalyst into the reaction kettle so as to reduce the occurrence of side reactions, the heating coil is used for adjusting the temperature in the 1# reaction kettle 1 to be in accordance with a set value by introducing steam so as to ensure that the ester exchange reaction is smoothly carried out, and the stirring device is beneficial to fully reacting waste oil and methanol under the action of the catalyst; the side surface of the upper part of the 1# precipitation kettle 2 is provided with a 1# precipitation kettle feed port h which is connected with a 1# reaction kettle 1 feed port e through a pipeline, the bottom of the 1# precipitation kettle 2 is provided with an automatic measurement densimeter 5 and a 1# precipitation kettle glycerol outlet i, the glycerol is precipitated at the bottom of the 1# precipitation kettle 2 due to high density, when the density reaches a set value, the glycerol is discharged from the 1# precipitation kettle glycerol outlet i through an automatic opening valve, and the side surface of the bottom of the 1# precipitation kettle 2 is provided with a 1# precipitation kettle feed port j; the side surface of the upper part of the 2# reaction kettle 3 is provided with a 2# reaction kettle feed inlet l which is connected with a 1# precipitation kettle feed inlet j through a pipeline, the top of the 2# reaction kettle is provided with a 2# reaction kettle catalyst feed inlet k, the bottom of the 2# reaction kettle feed inlet n is provided with a 2# reaction kettle feed inlet p, a 2# reaction kettle steam condensate outlet m and a 2# reaction kettle temperature measuring port o, the kettle is internally provided with a catalyst feed distribution disc, a steam coil pipe and a stirring device, and the action of the stirring device is the same as that of the 1# reaction kettle 1; since a portion of the catalyst was lost when the glycerin was discharged from the bottom of the 1# settling tank 2, the catalyst was replenished in the 2# reaction tank 3. 2# precipitation cauldron 4's upper portion side is equipped with 2# precipitation cauldron feed inlet q and 2# reation kettle material passing hole n pipe connection, another side is equipped with biodiesel export s, the bottom is equipped with automatic measure's densimeter and is equipped with 2# precipitation cauldron glycerine export r, when density reaches the setting value, through automatic opening valve, make 2# precipitation cauldron glycerine discharge from r, biodiesel then discharges from biodiesel export s, upper portion is equipped with intermediate bottom in the cauldron, it flows to make the material be the U type in 2# precipitation cauldron 4, be favorable to glycerine and biodiesel separation and discharge.
When the device is used, in order to ensure that waste oil, methanol, catalyst and biodiesel and glycerin generated in the reaction in the 1# reaction kettle 1 can smoothly flow into the 1# precipitation kettle 2, then automatically flow into the 2# reaction kettle 3, and finally automatically flow into the 2# precipitation kettle 4, the liquid level of the 1# reaction kettle 1 is required to be 0.3-0.5 meter higher than the liquid level of the 1# precipitation kettle 2, the liquid level of the 1# precipitation kettle 2 is required to be 0.3-0.5 meter higher than the liquid level of the 2# reaction kettle 3, and the liquid level of the 2# reaction kettle 3 is required to be 0.3-0.5 meter higher than the liquid level of the 2# precipitation kettle 4, so that a sufficient and reasonable liquid level difference between adjacent kettles is ensured.
The specific operation flow during production is as follows: feeding the waste oil, methanol and catalyst generated after the water separation in the esterification reaction into a No. 1 reaction kettle 1, starting stirring, introducing steam into a heating coil, reacting at a certain temperature, then enabling the materials to automatically flow into a No. 1 precipitation kettle 2 from the bottom of the No. 1 reaction kettle 1, and automatically discharging glycerin generated in the reaction through a densimeter at the bottom of the No. 1 precipitation kettle 2 so as to break the original ester exchange reaction balance and promote the reaction to proceed towards the direction of generating biodiesel; the material automatically flows into the No. 2 reaction kettle 3 from the bottom side surface of the No. 1 precipitation kettle 2, and because partial catalyst can be lost when the No. 1 precipitation kettle 2 discharges the glycerol, the catalyst needs to be supplemented in the No. 2 reaction kettle 3, and the reaction is continued under stirring; when the temperature does not meet the requirement, steam can be introduced into the heating coil to adjust the temperature to meet the set value; the material after the reaction automatically flows into the 2# settling kettle 4 from the bottom of the 2# reaction kettle 3 for settling separation, the glycerin is automatically discharged from the bottom of the 2# settling kettle 4 through the density meter, and the biodiesel flows out from the side surface of the upper part of the 2# settling kettle 4.
Claims (1)
1. A device for producing biodiesel by continuous ester exchange of waste oil and fat is characterized in that: the device comprises a No. 1 reaction kettle, a No. 1 precipitation kettle, a No. 2 reaction kettle, a No. 2 precipitation kettle and a connecting pipeline; the top of the No. 1 reaction kettle is provided with a waste oil inlet a, a No. 1 reaction kettle methanol inlet b and a No. 1 reaction kettle catalyst inlet c, the side surface of the No. 1 reaction kettle is provided with a No. 1 reaction kettle steam inlet g, a No. 1 reaction kettle steam condensate outlet d and a No. 1 reaction kettle temperature measuring port f, and the bottom of the No. 1 reaction kettle is provided with a No. 1 reaction kettle material passing port e; the reactor is internally provided with a catalyst feeding distribution disc, a heating coil and a stirring device, the catalyst distribution disc is beneficial to uniformly adding a catalyst into the reaction kettle so as to reduce the occurrence of side reactions, the heating coil is used for adjusting the temperature in the 1# reaction kettle to be in accordance with a set value by introducing steam so as to ensure that the ester exchange reaction is smoothly carried out, and the stirring device is beneficial to fully reacting waste oil and methanol under the action of the catalyst; the side surface of the upper part of the 1# precipitation kettle is provided with a 1# precipitation kettle feed port h which is connected with a 1# reaction kettle feed port e through a pipeline, the bottom of the 1# precipitation kettle is provided with an automatic measurement densimeter and a 1# precipitation kettle glycerol outlet i, and the side surface of the bottom of the 1# precipitation kettle is provided with a 1# precipitation kettle feed port j; the side surface of the upper part of the 2# reaction kettle is provided with a 2# reaction kettle feed port l which is connected with a 1# precipitation kettle feed port j through a pipeline, the top of the 2# reaction kettle is provided with a 2# reaction kettle catalyst feed port k, the bottom of the 2# reaction kettle is provided with a 2# reaction kettle feed port n, the side surface of the 2# reaction kettle is provided with a 2# reaction kettle steam inlet p, a 2# reaction kettle steam condensate outlet m and a 2# reaction kettle temperature measuring port o, and the kettle is internally provided with a catalyst feed distribution disc, a steam coil; 2# reation kettle's upper portion side is equipped with 2# precipitation cauldron feed inlet q and 2# reation kettle material passing hole n pipe connection, and another side is equipped with biodiesel export s, and automatic measuring densimeter is equipped with to the bottom and 2# precipitation cauldron glycerine export r is equipped with, and upper middle portion is equipped with intermediate bottom in the cauldron, makes the material be the U type in 2# precipitation cauldron and flows, is favorable to glycerine and biodiesel separation and discharge.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010206971.7A CN111234933A (en) | 2020-03-23 | 2020-03-23 | Device for producing biodiesel by continuous ester exchange of waste oil and fat |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010206971.7A CN111234933A (en) | 2020-03-23 | 2020-03-23 | Device for producing biodiesel by continuous ester exchange of waste oil and fat |
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|---|---|
| CN111234933A true CN111234933A (en) | 2020-06-05 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202010206971.7A Pending CN111234933A (en) | 2020-03-23 | 2020-03-23 | Device for producing biodiesel by continuous ester exchange of waste oil and fat |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112159729A (en) * | 2020-09-09 | 2021-01-01 | 湖北天基生物能源科技发展有限公司 | System for handle esterified oil |
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|---|---|---|---|---|
| CN2883376Y (en) * | 2006-02-15 | 2007-03-28 | 龙岩卓越新能源发展有限公司 | Biological diesel continuous prodn. plant |
| KR20100136876A (en) * | 2009-06-19 | 2010-12-29 | 박해영 | A method of continuously producing biological diesel oil |
| CN202116532U (en) * | 2011-06-24 | 2012-01-18 | 中国科学院广州能源研究所 | Biodiesel continuous ester exchange production equipment |
| CN104419526A (en) * | 2013-09-02 | 2015-03-18 | 河南隆正生物能源有限公司 | Device for producing biodiesel from waste catering oil |
| CN104651060A (en) * | 2015-02-03 | 2015-05-27 | 江苏西方环保科技有限公司 | Biodiesel continuous ester interchange technology |
| CN204897878U (en) * | 2015-08-17 | 2015-12-23 | 龙岩卓越新能源股份有限公司 | Useless oil and fat preparation biodiesel's continuous esterification column device |
| CN110093212A (en) * | 2019-04-23 | 2019-08-06 | 龙岩卓越新能源股份有限公司 | A kind of method of waste oil continuous esterification production |
| CN212051293U (en) * | 2020-03-23 | 2020-12-01 | 龙岩卓越新能源股份有限公司 | Device for producing biodiesel by continuous ester exchange of waste oil and fat |
-
2020
- 2020-03-23 CN CN202010206971.7A patent/CN111234933A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2883376Y (en) * | 2006-02-15 | 2007-03-28 | 龙岩卓越新能源发展有限公司 | Biological diesel continuous prodn. plant |
| KR20100136876A (en) * | 2009-06-19 | 2010-12-29 | 박해영 | A method of continuously producing biological diesel oil |
| CN202116532U (en) * | 2011-06-24 | 2012-01-18 | 中国科学院广州能源研究所 | Biodiesel continuous ester exchange production equipment |
| CN104419526A (en) * | 2013-09-02 | 2015-03-18 | 河南隆正生物能源有限公司 | Device for producing biodiesel from waste catering oil |
| CN104651060A (en) * | 2015-02-03 | 2015-05-27 | 江苏西方环保科技有限公司 | Biodiesel continuous ester interchange technology |
| CN204897878U (en) * | 2015-08-17 | 2015-12-23 | 龙岩卓越新能源股份有限公司 | Useless oil and fat preparation biodiesel's continuous esterification column device |
| CN110093212A (en) * | 2019-04-23 | 2019-08-06 | 龙岩卓越新能源股份有限公司 | A kind of method of waste oil continuous esterification production |
| CN212051293U (en) * | 2020-03-23 | 2020-12-01 | 龙岩卓越新能源股份有限公司 | Device for producing biodiesel by continuous ester exchange of waste oil and fat |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112159729A (en) * | 2020-09-09 | 2021-01-01 | 湖北天基生物能源科技发展有限公司 | System for handle esterified oil |
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