CN102787022A - Reaction system for countercurrent continuous esterification of biodiesel - Google Patents
Reaction system for countercurrent continuous esterification of biodiesel Download PDFInfo
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- CN102787022A CN102787022A CN2012101795030A CN201210179503A CN102787022A CN 102787022 A CN102787022 A CN 102787022A CN 2012101795030 A CN2012101795030 A CN 2012101795030A CN 201210179503 A CN201210179503 A CN 201210179503A CN 102787022 A CN102787022 A CN 102787022A
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- reaction tower
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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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Abstract
The invention discloses a reaction system for countercurrent continuous esterification of biodiesel. The system comprises a raw material storage tank, a methanol storage tank, at least one first reaction tower and at least one second reaction tower, and at least one separator connected between a reaction product outlet of the first reaction tower and a material inlet of the second reaction tower. The raw material storage tank is connected to a catalyst storage tank and a material inlet at the upper part of the first reaction tower; the methanol storage tank is connected to a methanol inlet at a lower part of the second reaction tower; and a methanol outlet at the top of the second reaction tower is connected to a methanol inlet at the bottom of the first reaction tower. The invention realizes countercurrent esterification of biodiesel, and real-time reaction and separation of glycerol, water and methanol, greatly shortens the reaction time, and achieves thorough reaction.
Description
Technical field
The present invention relates to chemical field, relate to a kind of biofuel adverse current continuous esterification system particularly, its esterification that is particularly suitable for the production of biodiesel process is used.
Background technology
Biofuel (Biodiesel) is meant the reproducibility diesel oil fuel with waterplant greases such as oil crops, wild oilseed plant and engineering microalgae and animal oil and fat, food garbage wet goods the replaced petrifaction diesel that to be raw oil process through ester exchange process.Biofuel is a kind of of biomass energy, and it is the mono alkyl ester that biomass are utilized a kind of longer chain fatty acid that technology such as thermo-cracking obtain.Biofuel is the mixture of the high complicated organic composition of oxygen level, and these mixtures mainly are the big organism of number molecular weight, almost comprises the oxygen-bearing organic matter of all kinds, as: ether, ester, aldehyde, ketone, phenol, organic acid, alcohol etc.
Raw oil material adds excessive methanol, in the presence of an acidic catalyst, carries out esterification, makes free acid be transformed into crude fatty acid methyl ester.In the prior art, the esterification that generates crude fatty acid methyl ester all is to adopt the still reaction device, when heating; Stir with whisking appliance and to promote the carrying out that react, but because can not continuous production, and grease is incompatible with methyl alcohol; Its long reaction time; Esterification is incomplete, and energy consumption is high, makes that the biofuel cost of producing is high.
Summary of the invention
The object of the present invention is to provide biofuel adverse current continuous esterification system, to solve the problems referred to above that exist in the prior art.
Technical scheme provided by the invention is following:
Biofuel adverse current continuous esterification system is characterized in that, comprising:
One raw material storage tank, a methyl alcohol storage tank;
At least one first reaction tower, its top are provided with at least one material inlet and methyl alcohol outlet, and the bottom is provided with an at least one reacting product outlet and a methyl alcohol import;
At least one second reaction tower, its top are provided with at least one material inlet and methyl alcohol outlet, and the bottom is provided with an at least one reacting product outlet and a methyl alcohol import;
At least one methanol rectifying tower
The separation storage tank is all arranged at its each reaction tower bottom;
Wherein, described raw material storage tank is connected with the material inlet on the first reaction tower top, and the methyl alcohol import of the described methyl alcohol storage tank and the bottom of second reaction tower is connected, and the methyl alcohol outlet at the second reaction tower top is connected with the methyl alcohol import of first reaction tower bottom again.The outlet of first methyl alcohol is connected with methanol column.
In preferred embodiment of the present invention, be connected with gauger between the outlet of described methyl alcohol storage tank and second reaction tower.
In preferred embodiment of the present invention, be connected with gauger between the described raw material storage tank and first reaction tower.
In preferred embodiment of the present invention, be provided with filler in described first reaction tower or second reaction tower, be provided with scum dredger in the cat head.This filler is used for contacting of material and methyl alcohol, and this scum dredger is used for avoiding impurity to bring the methyl alcohol of recovery into.
In preferred embodiment of the present invention, also be connected with well heater between the outlet of described methyl alcohol storage tank and second reaction tower.
In preferred embodiment of the present invention, be provided with enamel layer in described first reaction tower and second reaction tower.
In preferred embodiment of the present invention, the reaction tower bottom is provided with the separation reservoir of separation system.
The present invention gets into the reactor drum upper end with the raw material of neutral vegetable and animals oils and free fatty acids through under meter; Dirty along filler; The vaporization of low-carbon alcohol heater via contacts and reaction at filling surface under the condition that catalyzer exists or under the catalyst-free medium temperature condition after reactor drum lower end edge filler adverse current is up.The water that reaction generates goes to return repetition after the Methanol Recovery purification through the upper end outlet with methyl alcohol, and reacted mixed solution through the lower end separator tank isolate glycerine and the impurity etc. of generation.The subordinate phase reaction is on the basis of first set reaction, to have separated to carry out same operation behind the impurity.Reacted aqueous methanol is returned repeated use after getting into the methanol rectifying tower dehydration.
Because the water that material fully contacts under inner-tower filling material and generates with methyl alcohol is in time separated, feasible reaction is carried out to positive dirction with high-level efficiency all the time, and reaction is comparatively thorough and quick.Realize the real-time separation and the reaction of biofuel adverse current esterification, glycerine, water, methyl alcohol, shortened the reaction times greatly.In addition, be provided with enamel layer in the reaction tower, equipment is not perishable.The present invention has broken away from the limitation that traditional biological diesel oil is reflected at the stirring-type reaction kettle.And tandem is organized the maximized energy of having practiced thrift of countercurrent reaction system more, meets reaction mechanism more.
Description of drawings
Fig. 1 is the structural representation of biofuel adverse current continuous esterification of the present invention system.
Among the figure: 1-raw material storage tank 11 gaugers
2-methyl alcohol storage tank 21 gaugers
3-first reaction tower
31 fillers, 32 scum dredgers, 33 methyl alcohol export the outlet of 34 material inlets, 35 reacting product outlets, 36 methyl alcohol imports, 37 spargers, 38 sloping baffles, 39 sub products
The 4-second reaction tower 5-methanol rectifying tower 6-well heater 7-well heater 8-well heater 9-condensing surface
Embodiment
Specific embodiment of the present invention, with reference to Fig. 1, biofuel adverse current continuous esterification system comprises raw material storage tank 1, methyl alcohol storage tank 2, first reaction tower 3, second reaction tower 4, methanol rectifying tower 5, well heater 6,7,8 etc.
These first reaction tower, 3 tops are provided with a material inlet 34 and methyl alcohol outlet 33, and the bottom is provided with a reacting product outlet 35 and a methyl alcohol import 36; Its inside is provided with filler 31, and inner top is provided with scum dredger 32.The reaction tower bottom is provided with the separation reservoir of separation system, and it comprises the sloping baffle 38 of being located at distributor 37 belows, and reacting product outlet 35 is located at sidewall, and the bottom surface is located in sub product outlet 39.
The structure of this second reaction tower 4 is identical with the structure of first reaction tower 3.
The outlet heater via 6 of raw material storage tank 1 is connected with the material inlet 34 of first reaction tower 3, is provided with gauger 11 in the exit of raw material storage tank 1;
The methyl alcohol import heater via 7 of second reaction tower 4 is connected with methyl alcohol storage tank 2, and the methyl alcohol outlet at second reaction tower, 4 tops is connected with the methyl alcohol import 36 of first reaction tower, 3 bottoms again.
Connect through a dehvery pump between the reacting product outlet 35 of first reaction tower 3 and the material inlet at the second reaction tower top.Top methyl alcohol outlet is connected with the methyl alcohol import of methanol rectifying tower 5.
Principle of work of the present invention is following: raw material such as vegetable and animals oils pump heater via 6 and get into first reaction tower 3 from raw material storage tank 1; The filler 31 of cistron tower 3 inside is to dirty; And methyl alcohol from methyl alcohol storage tank 2 behind gauger 21; Elder generation is got in the reaction tower through second reaction tower, 4 spargers by well heater 7 heating again, the distributor 37 that after top of tower is discharged, gets into first reaction tower 3, and filler 31 adverse currents of cistron tower 3 inside are up; Raw material and methyl alcohol contact and react through filling surface under 80C ° to 250C ° condition; React the water and methyl alcohol outlet 33 discharges from the upper end of residue methyl alcohol that generate, methyl alcohol is back to methyl alcohol storage tank 2 after methanol rectifying tower 5 reclaims purification, and reacted mixed solution gets into second reaction tower 4 at reacting product outlet 35 through dehvery pump; Again with the reaction of fresh methyl alcohol, by this can the raw material of complete reaction not is complete through single step reaction.
Above-mentionedly be merely specific embodiment of the present invention, but design concept of the present invention is not limited thereto, allly utilizes this design that the present invention is carried out the change of unsubstantiality, all should belong to the behavior of invading protection domain of the present invention.
Claims (7)
1. biofuel adverse current continuous esterification system is characterized in that, comprising:
One raw material storage tank, a methyl alcohol storage tank;
At least one first reaction tower, its top are provided with at least one material inlet and methyl alcohol outlet, and the bottom is provided with an at least one reacting product outlet and a methyl alcohol import;
At least one second reaction tower, its top are provided with at least one material inlet and methyl alcohol outlet, and the bottom is provided with an at least one reacting product outlet and a methyl alcohol import;
At least one separator, it is connected between the material inlet of reacting product outlet and second reaction tower of first reaction tower;
Wherein, described raw material storage tank is connected with the material inlet on the first reaction tower top, and the methyl alcohol import of the described methyl alcohol storage tank and the bottom of second reaction tower is connected, and the methyl alcohol outlet at the second reaction tower top is connected with the methyl alcohol import of first reaction tower bottom again.
2. biofuel adverse current continuous esterification as claimed in claim 1 system is characterized in that: be connected with gauger between the outlet of described methyl alcohol storage tank and second reaction tower.
3. biofuel adverse current continuous esterification as claimed in claim 1 system is characterized in that: be connected with gauger between the described raw material storage tank and first reaction tower.
4. biofuel adverse current continuous esterification as claimed in claim 1 system is characterized in that: be provided with filler in described first reaction tower or second reaction tower, be provided with scum dredger in the cat head.
5. biofuel adverse current continuous esterification as claimed in claim 1 system is characterized in that: also be connected with well heater between the outlet of described methyl alcohol storage tank and second reaction tower.
6. like each described biofuel adverse current continuous esterification system of claim 1 to 5, it is characterized in that: be provided with enamel layer in described first reaction tower and second reaction tower.
7. like each described biofuel adverse current continuous esterification system of claim 1-5, it is characterized in that: the reaction tower bottom is provided with the separation reservoir of separation system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012101795030A CN102787022A (en) | 2012-05-08 | 2012-05-30 | Reaction system for countercurrent continuous esterification of biodiesel |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201220203131.6 | 2012-05-08 | ||
| CN201220203131 | 2012-05-08 | ||
| CN2012101795030A CN102787022A (en) | 2012-05-08 | 2012-05-30 | Reaction system for countercurrent continuous esterification of biodiesel |
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| CN102787022A true CN102787022A (en) | 2012-11-21 |
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| CN2012202577289U Expired - Fee Related CN202643671U (en) | 2012-05-08 | 2012-05-30 | Biodiesel counter-flow continuous esterification reaction system |
| CN2012101795030A Pending CN102787022A (en) | 2012-05-08 | 2012-05-30 | Reaction system for countercurrent continuous esterification of biodiesel |
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| CN2012202577289U Expired - Fee Related CN202643671U (en) | 2012-05-08 | 2012-05-30 | Biodiesel counter-flow continuous esterification reaction system |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104031747A (en) * | 2014-06-13 | 2014-09-10 | 太原理工大学 | Production device and method of biodiesel |
| CN104830543A (en) * | 2015-04-28 | 2015-08-12 | 广东河山环保有限公司 | Device and method for preparing biodiesel through continuous gas-phase catalytic esterification |
| CN105176697A (en) * | 2015-08-17 | 2015-12-23 | 龙岩卓越新能源股份有限公司 | Continuous esterification column apparatus for preparing biodiesel from waste fat and oil |
| CN105586154A (en) * | 2015-12-31 | 2016-05-18 | 陕西合盛生物柴油技术开发有限公司 | Continuous esterification method for preparing biodiesel from waste grease |
| CN107099381A (en) * | 2017-04-10 | 2017-08-29 | 中国科学院广州能源研究所 | Biodiesel prepares reaction unit |
| CN110773103A (en) * | 2019-09-20 | 2020-02-11 | 韩志彬 | Normal-pressure catalysis-free tower type continuous esterification production equipment and production process |
| CN111234932A (en) * | 2020-02-12 | 2020-06-05 | 常州市金坛区维格生物科技有限公司 | Method for preparing biodiesel by continuous countercurrent esterification reaction |
| CN112588281A (en) * | 2020-12-16 | 2021-04-02 | 华润环保发展有限公司 | Preparation method of catalyst and reaction device applied by same |
| CN115845758A (en) * | 2021-09-24 | 2023-03-28 | 浙江医药股份有限公司新昌制药厂 | Continuous reaction device and method for preparing phosphoric acid diester compound through continuous reaction |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202643671U (en) * | 2012-05-08 | 2013-01-02 | 种传学 | Biodiesel counter-flow continuous esterification reaction system |
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| CN101781610A (en) * | 2010-03-16 | 2010-07-21 | 刘宽 | Continuous esterification and ester exchange process used for producing biodiesel |
| CN101892127A (en) * | 2010-05-13 | 2010-11-24 | 昆明理工大学 | Biodiesel preparation method |
| CN202099261U (en) * | 2011-05-12 | 2012-01-04 | 种传学 | Esterification and directional separation integrated device for biodiesel production |
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2012
- 2012-05-30 CN CN2012202577289U patent/CN202643671U/en not_active Expired - Fee Related
- 2012-05-30 CN CN2012101795030A patent/CN102787022A/en active Pending
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| CN101781610A (en) * | 2010-03-16 | 2010-07-21 | 刘宽 | Continuous esterification and ester exchange process used for producing biodiesel |
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| CN102344857A (en) * | 2010-08-06 | 2012-02-08 | 无锡市正洪生物柴油设备科技有限公司 | Mobile multi-set serial fixed bed solid acid biodiesel production equipments and technological process |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104031747A (en) * | 2014-06-13 | 2014-09-10 | 太原理工大学 | Production device and method of biodiesel |
| CN104031747B (en) * | 2014-06-13 | 2016-02-24 | 太原理工大学 | A kind of production equipment of biofuel and production method |
| CN104830543A (en) * | 2015-04-28 | 2015-08-12 | 广东河山环保有限公司 | Device and method for preparing biodiesel through continuous gas-phase catalytic esterification |
| CN105176697A (en) * | 2015-08-17 | 2015-12-23 | 龙岩卓越新能源股份有限公司 | Continuous esterification column apparatus for preparing biodiesel from waste fat and oil |
| CN105586154A (en) * | 2015-12-31 | 2016-05-18 | 陕西合盛生物柴油技术开发有限公司 | Continuous esterification method for preparing biodiesel from waste grease |
| CN107099381A (en) * | 2017-04-10 | 2017-08-29 | 中国科学院广州能源研究所 | Biodiesel prepares reaction unit |
| CN110773103A (en) * | 2019-09-20 | 2020-02-11 | 韩志彬 | Normal-pressure catalysis-free tower type continuous esterification production equipment and production process |
| CN111234932A (en) * | 2020-02-12 | 2020-06-05 | 常州市金坛区维格生物科技有限公司 | Method for preparing biodiesel by continuous countercurrent esterification reaction |
| CN112588281A (en) * | 2020-12-16 | 2021-04-02 | 华润环保发展有限公司 | Preparation method of catalyst and reaction device applied by same |
| CN115845758A (en) * | 2021-09-24 | 2023-03-28 | 浙江医药股份有限公司新昌制药厂 | Continuous reaction device and method for preparing phosphoric acid diester compound through continuous reaction |
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| CN202643671U (en) | 2013-01-02 |
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Application publication date: 20121121 |