CN202912929U - Continuous production equipment for biodiesel - Google Patents
Continuous production equipment for biodiesel Download PDFInfo
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- CN202912929U CN202912929U CN2012205380268U CN201220538026U CN202912929U CN 202912929 U CN202912929 U CN 202912929U CN 2012205380268 U CN2012205380268 U CN 2012205380268U CN 201220538026 U CN201220538026 U CN 201220538026U CN 202912929 U CN202912929 U CN 202912929U
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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 utility model discloses continuous production equipment for biodiesel, which comprises a biodiesel reaction device, a connecting pipeline, as well as a metering pump, a delivery pump and a flow meter inside a pipeline, wherein the biodiesel reaction device comprises a mixer (2), a heater I (3), a pipeline reaction I (4), an esterification reaction tower (5), a catalyst separator (10), a methanol storage tank (9), a methanol alkali liquor tank (12), a pipeline reactor II (24), a flash tower (15), a glycerol separator (16), a distillation tower (17) and a biodiesel storage tank (19). The equipment provided by the utility model has a wide application range to the quality of base oil, the production energy consumption is low, the conversion rate is higher, the environmental friendliness can be achieved, and the product quality and the productivity of the biodiesel can be improved more efficiently.
Description
Technical field
The utility model belongs to the production of biodiesel field, particularly a kind of continuous producing apparatus of biofuel.
Background technology
Along with the sharp increase of people to the petroleum chemicals demand, to Nonrenewable resources---the produced quantity of oil also increases gradually, so that the reserves of this Nonrenewable resources reduce day by day, although new oil-gas field is constantly arranged to be verified, but based on the demand consideration in future, petroleum resources will be exhausted within coming few decades.Therefore seeking reproducible substitute, will be the direction of WeiLai Technology development.
The biofuel main component is fatty acid methyl ester (or ethyl ester), the green regenerative energy sources of making as raw material take animal oil, vegetables oil, compare with petrifaction diesel have good combustionproperty, lubricity, safety performance, excellent environmental friendliness performance and renewable performance.
Because the supply of the animal-plant oil of China is more in short supply, State Council expressly provides and forbids adopting the animals and plants food oils as the raw material production biofuel, therefore, domestic can only be with the stock oil of the greases such as discarded animal-plant oil, non-edible woody oleiferous plants as biofuel.The biodiesel raw material of China is mainly take high acid value vegetable and animals oils such as sewer oil, hogwash fat, soybean acidified oil, palmitinic acid carburetion as main at present, the free fatty acid content of these stock oils is higher, and the quality of oil plant alters a great deal, and general acid number is between 20～150mgKOH/g.
Stock oil for high acid value mainly adopts esterification, transesterify two-step approach production biofuel.Esterification is reversible reaction, and the water that reaction generates can suppress the carrying out of esterification, thereby reduces the transformation efficiency of esterification.The effective ways of industrial raising esterification transformation efficiency mainly are that the method for the method that adds excessive methanol, sedimentation draining and the method by methyl alcohol band water remove the water that esterification generates.About production equipment and the technology of preparing of biofuel, we find following related data:
1. application number: 200920000084.3, a kind of production unit of refining biodiesel is disclosed, comprise reactor, fuel oil preheating tank, catalyzer methanol mixed device and methanol recovery device with some imports and outlet, the high-quality height of biofuel that this equipment can be produced continuously and produce, the advantage such as production process is pollution-free; Application number: 98811443.7, method and the production unit of producing fatty acid methyl ester are disclosed, have and can accomplish not only with ecological best but also keep its working condition that is possessed some good points to produce diesel oil fuel.There is a common shortcoming in these two patent production units, namely be too narrow to the scope of application of stock oil, can only be take neutral grease such as animal grease, Vegetable oil lipoprotein as the raw material production biofuel, can not prepare biofuel take sewer oil, the contour acid number grease of acidification oil as raw material.And domestic mainly be as raw material at present take high-acid value grease.
2. application number: 200620019343.3, a kind of device for preparing biofuel is disclosed, this device is by methanol gasifying device (1), by pipeline (51) and T-valve (8), (50), (46) esterification that is connected with methanol gasifying device (1), transesterification reactor (24), by pipeline (42) and two-port valve (45) and esterification, transesterification reactor (23) connects steam evaporator (24), by air pressure balance passage (27), the water-and-oil separator (28) that pipeline (39) and two-port valve (38) are connected with steam generator (24), by air pressure balance passage (30), the biofuel collector (31) of two-port valve (36) is equipped with in its underpart that biofuel discharge outlet (32) is connected with water-and-oil separator (28), and the product biofuel storage tank (34) that is connected with biofuel collector (31) by pipeline (35) and two-port valve (33) forms.This device has compact construction, and cost is low, and versatility, handiness and the feature of environmental protection are good, the raw material of suitable various qualities, and its shortcoming is: the contact area of liquid phase grease and gas-phase methanol is little, and the utilization ratio of methyl alcohol is low, long reaction time, energy consumption is higher.
3. application number: 200710019278.3, the reactor of making biofuel is disclosed, comprise kettle and the whipping appts that is installed on the kettle, described kettle is tool jacket type structure with dissection, steam inlet on the kettle and condensation-water drain communicate with interlayer, the material inlet that is respectively equipped with on the kettle, discharge port, catalyst inlet and solvent inlet communicate with the kettle reaction chamber, described material inlet and catalyst inlet are separately positioned on kettle top, opening for feed is arranged on the bottom of kettle, and solvent inlet is arranged on the bottom of kettle or/and the bottom.The reactor of this invention is simple in structure, and facility investment is few, and esterification is abundant, and production efficiency is high, can satisfy commercial scale production.But when this reactor was used for esterification, the water that esterification generates can not be separated from reaction system, and the existence of water can suppress the carrying out of esterification, causes conversion rate of esterification lower, and the biofuel utilization ratio is also lower.
4. application number: 200820081719, disclose novel production of biodiesel reaction tower, its reaction tower 2 tops are provided with the methanol steam outlet pipe 1 that passes in the tower, stock oil and catalyst inlet pipe 3, inside is provided with foam removal dish 4, lack arc and hide stream transverse slat 5, the bottom is provided with the methanol steam inlet tube 7 that passes in the tower, products export pipe 8, pipe pump 9, return line 10, this return line passes into the top of tower, is provided with valve on each inlet/outlet pipe road junction.The contact area of this utility model gas-phase methanol and oil phase is than the to some extent increase of tank reactor, but the amplitude that improves is limited, and the utilization ratio of methyl alcohol is lower, the reaction times or long, energy consumption is also high, and reaction mass needs to react at the reaction tower internal recycle for a long time.
5. application number: 200810163740, a kind of method for preparing biofuel take high-acid value grease as raw material is disclosed, with the various animal-plant oil of acid number greater than 3.0mg KOH/g oil, and oil foot, soap stock, acidification oil in the refining process of vegetables oil; Various edible waste oil (waste cooking oil, hogwash fat, trench wet goods), various discarded animal grease in the industrial processes process (the useless animal grease in the leather processing procedure, the useless animal grease in the slaughtering process etc.) is raw material, removes after filtration solid impurity, vacuum hydro-extraction, hierarchical layered acid catalyzed esterification, base-catalyzed transesterification, vacuum distilling and obtains the biofuel product.The utility model beneficial effect is mainly reflected in: adopt production technique described in the utility model, by changing the operation progression of hierarchical layered esterification, the raw material that can adapt to different acid numbers, produce highly purified biofuel product, and technique is simple, energy consumption is low, speed is fast, transformation efficiency is high, equipment is little, and can realize serialization production.But its shortcoming is to produce into a large amount of acid waste waters, and the various production efficiency of operation is low.
Summary of the invention
The purpose of this utility model is in order to overcome the deficiencies in the prior art, a kind of continuous producing apparatus of less energy-consumption biofuel to be provided.The utility model is applied widely to the stock oil quality, and production energy consumption is low, and transformation efficiency is higher, more environmental protection, quality product and the productive rate of the more effective raising biofuel of energy.
In order to achieve the above object, the utility model is achieved through the following technical solutions:
A kind of continuous producing apparatus of biofuel, comprise the biofuel reaction unit, connecting tube and ducted volume pump, transferpump and under meter, described biofuel reaction unit comprises mixing tank, the well heater I, the pipeline reactor I, esterification reaction tower, catalyst separator, the methyl alcohol basin, the rosaline flow container, the pipeline reactor II, flashing tower, glycerin separator, distillation tower and biofuel basin, mixer outlet is connected with the pipeline reactor I by the well heater I, pipeline reactor I outlet conduit is connected with the esterification reaction tower upper inlet, and the esterification reaction tower outlet at bottom is communicated with catalyst separator; Described methyl alcohol basin outlet is connected with the import of rosaline flow container, the outlet of rosaline flow container is connected the volume pump that passes through separately and is connected with the pipeline reactor II with catalyst separator top, pipeline reactor II outlet conduit connects the flashing tower upper inlet, flashing tower outlet at bottom pipeline connects the glycerin separator lower inlet, the outlet of glycerin separator top connects the distillation tower bottom, and the distillation tower top exit is connected with the biofuel basin.
Be provided with spiral plate in the above pipeline reactor, spiral plate is provided with the traverse baffle that staggers mutually, when reaction mass passes through pipeline reactor, utilizes traverse baffle can increase the turbulence intensity of reaction mass, improves mixed effect.
Be provided with bubble trap, flasher, falling film evaporator and packing tower in the above esterification reaction tower from top to bottom, described esterification reaction tower upper inlet is located between bubble trap and the flasher, and described esterification reaction tower lower inlet is located at the packing tower below.The effect of flasher is to remove the remaining most of methyl alcohol of one-level esterification and part water; The effect of falling film evaporator is: the one, in order to prevent that material from steaming through the first in the material behind the flasher of cat head and water does not eliminate, further remove, guarantee material enter conversion zone after water-content enough low; The 2nd, provide heat to material, make the technological temperature of grease temperature appointment, guarantee that the water that esterification produces in the conversion zone can be evaporated from oil phase; The effect of packing tower is to increase pure oily contact area, improves speed of reaction and methanol conversion.
Above-described packing tower be by fiber, silk screen, Pall ring, conjugate ring, cascade ring and flat ring in any one or a few packing tower that consists of.
The continuous producing apparatus of the above biofuel also comprises methanol recovery device, methanol recovery device comprises methanol rectifying tower and condenser, the methanol rectifying tower lower inlet is connected with esterification reaction tower top exit pipeline, the methanol rectifying tower top duct is provided with two outlets, an outlet is connected with the esterification reaction tower lower inlet through pipeline connection traffic meter I, another outlet is connected with the import of methyl alcohol basin by the condenser I through pipeline connection traffic meter II road, and another import of methyl alcohol basin is connected with the flashing tower top exit by the condenser II.
Be provided with the well heater II between the above pipeline reactor II and the flashing tower.
Be provided with the condenser III between the above distillation tower and the biofuel basin.
The above glycerin separator outlet at bottom pipeline is connected with the glycerine basin.
The above catalyst separator outlet at bottom pipeline is connected with an acidic catalyst withdrawing can.
The principle of work that the utility model prepares biofuel is as follows:
Methyl alcohol, an acidic catalyst and stock oil pump into mixing tank by volume pump separately respectively, after mixing tank carries out the height mixing, by well heater reaction mass is heated to certain temperature again, material after the intensification enters the pipeline reactor I and carries out esterification, continue heat temperature raising at pipeline reactor I internal reaction material, the built-in special volution of pipeline reactor I and with the motionless mixer of traverse baffle, when reaction mass passes through the pipeline reactor I, utilize motionless mixer to make reaction mass continue to mix, traverse baffle on the mixing tank can increase the turbulence intensity of reaction mass, improves mixed effect.
After the esterification of pipeline reactor I one-level, reaction mass enters esterification reaction tower from the opening for feed on esterification reaction tower top, methanol steam enters esterification reaction tower from the methyl alcohol import of reaction tower bottom simultaneously, reaction mass is at the water of removing the generation of most superfluous methyl alcohol and esterification by the flasher on esterification reaction tower top, remove residual first alcohol and water by falling film evaporator again, and temperature of charge is brought up to the technological temperature of setting, material enters packing tower after by falling film evaporator, material is evenly distributed on the filler, and form liquid film at filling surface, contact with the methanol steam that rises and esterification occurs, the water that esterification generates is taken from liquid phase reacting material by the methanol steam of surplus, flow out from the outlet of esterification column reaction cat head, and enter methanol rectifying tower from the opening for feed of methanol rectifying tower, through methanol rectifying tower separate anhydrate minute after, distillate from tower top outlet, a part is back to esterification reaction tower through the under meter I and carries out esterification, by the amount that the control of under meter I refluxes, a part enters the methyl alcohol basin after the condensation of condenser I; Outlet at the bottom of the reaction tower is flowed out through the material after the esterification reaction tower esterification, enter catalyst separator and carry out an acidic catalyst and esterification oil separating, isolated catalyzer enters an acidic catalyst withdrawing can from the separator outlet at bottom, esterised oil flows out from the outlet of catalyst separator top, be metered into the pipeline reactor II by the volume pump III, the basic catalyst methyl alcohol that contains in the rosaline flow container is metered into the pipeline reactor II by the volume pump II simultaneously, reaction mass carries out transesterification reaction in the pipeline reactor II, after finishing transesterification reaction, material is through well heater II heat temperature raising, entering flashing tower carries out flash distillation and removes excessive methyl alcohol, methanol steam enters the methyl alcohol basin after passing through the condensation of condenser II by the flashing tower tower top outlet, oil plant after the dealcoholysis pumps into glycerin separator through the transferpump I and carries out glycerine, separating of basic catalyst and grease, after separating, glycerine and basic catalyst enter the glycerine basin, the coarse biodiesel that separation obtains enters distillation tower and carries out distilation, the biofuel steam that distillates of cat head enters the biofuel basin after the condensation of condenser III, the remaining heavy oil distillation tower of distillation enters heavy oil service tank.
Compared with prior art, the beneficial effects of the utility model are:
1. esterification adopts the method for liquid phase reaction and vapour-phase reaction coupling to carry out continuous esterification.Acid number at the one-level esterification stock oil that acid number is widely different is reduced to lower level, has guaranteed that the secondary esterification once just can be reduced to acid number below the 1mgKOH/g by esterification column.This processing method is stronger to the adaptive faculty of stock oil, and technique is more stable, and the continuity of production is stronger.
2. reaction mass directly enters esterification column by behind the pipeline reactor, does not need to add in addition pump and carries, and does not also need to carry out separately Methanol Recovery.Esterification column is divided into the esterification reaction section of flash distillation, falling film evaporation dealcoholysis, dewatering period and the bottom of part, and this processing method has reduced troublesome operation, time and the power consumption of dealcoholysis, dehydration.
3. liquid phase reacting material advances that the form with liquid film contacts with the methanol steam of convection current on the filler of esterification column, and pure oily contact area is large, and reaction efficiency is high, and the methanol steam utilization ratio is high.
4. aqueous methanol steam flows out from the esterification reaction tower top, directly enter methanol fractionation system carry out pure moisture from, the methanol steam behind minute water need not carry out condensation, cooling, directly gets back to esterification column and carries out esterification.Heat energy is utilized effectively, and significantly reduces production energy consumption.
Glycerine after the separation of an acidic catalyst after the esterification and the transesterify separate all adopt knockout tower carry out continuous separate from, separation efficiency is high, energy consumption is low.
6. extremely low from the isolated an acidic catalyst water content of knockout tower, can use by direct repeat, must not make in addition processed.
7. do not produce acid waste water, production technique is environmental protection very.
Description of drawings
Fig. 1 is the continuous production device structural representation of the utility model biofuel;
Fig. 2 is the structural representation of pipeline reactor;
Reference numeral:
1-volume pump I, 2-mixing tank, 3-well heater I, 4-pipeline reactor I, the 5-esterification reaction tower, 6-under meter I, 7-under meter II, the 8-methanol rectifying tower, 9-methyl alcohol basin, 10-catalyst separator, 11-condenser I, 12-rosaline flow container, 13-condenser II, 14-well heater II, 15-flashing tower, 16-glycerin separator, the 17-distillation tower, 18-condenser III, 19-biofuel basin, the 20-heavy oil service tank, 21-glycerine basin, 22-transferpump I, 23-transferpump II, 24-pipeline reactor II, 25-volume pump II, 26-volume pump III, 27-an acidic catalyst withdrawing can, 28-transferpump III, 29-volume pump IV, 30-spiral plate, 31-traverse baffle;
5.1-bubble trap, 5.2-flasher, 5.3-falling film evaporator, 5.4-packing tower.
Implementation side
Below in conjunction with embodiment the utility model is described in further detail, but embodiment of the present utility model is not limited to the scope that embodiment represents.
Embodiment 1:
A kind of continuous producing apparatus of biofuel, comprise the biofuel reaction unit, methanol recovery device, connecting tube and ducted volume pump, transferpump and under meter, its biofuel reaction unit comprises mixing tank 2, well heater I 3, pipeline reactor I 4, esterification reaction tower 5, catalyst separator 10, methyl alcohol basin 9, rosaline flow container 12, pipeline reactor II 24, flashing tower 15, glycerin separator 16, distillation tower 17 and biofuel basin 19, mixing tank 2 outlets are connected with pipeline reactor I 4 by well heater I 3, pipeline reactor I 4 outlet conduits are connected with esterification reaction tower 5 upper inlet, esterification reaction tower 5 outlet at bottoms are communicated with catalyst separator 10, and catalyst separator 10 outlet at bottom pipelines are connected with an acidic catalyst withdrawing can 27; 9 outlets of methyl alcohol basin are connected with 12 imports of rosaline flow container, rosaline flow container 12 outlet is connected the volume pump that the top outlet passes through separately and is connected with pipeline reactor II 24 with catalyst separator, pipeline reactor II 24 outlet conduits connect flashing tower 15 upper inlet, be provided with well heater II 14 between pipeline reactor II 24 and the flashing tower 15, flashing tower 15 outlet at bottom pipelines connect glycerin separator 16 lower inlet, glycerin separator 16 outlet at bottom pipelines are connected with glycerine basin 21, the outlet of glycerin separator 16 tops connects distillation tower 17 bottoms, distillation tower 17 top exits are connected with biofuel basin 19, are provided with condenser III 18 between distillation tower 17 and the biofuel basin 19.
Methanol recovery device comprises methanol rectifying tower 8, condenser I 11 and condenser II 13, methanol rectifying tower 8 lower inlet are connected with esterification reaction tower 5 top exit pipelines, methanol rectifying tower 8 top ducts are provided with two outlets, an outlet is connected with esterification reaction tower 5 lower inlet through pipeline connection traffic meter I 6, another outlet is connected with 9 imports of methyl alcohol basin by condenser I 11 through pipeline connection traffic meter II 7 roads, and 9 another imports of methyl alcohol basin are connected with flashing tower 15 top exits by condenser II 13.
Be provided with spiral plate 30 in pipeline reactor I 4 and the II 24, spiral plate 30 is provided with the traverse baffle 31 that staggers mutually.
Be provided with bubble trap 5.1, flasher 5.2, falling film evaporator 5.3 and packing tower 5.4 in the esterification reaction tower 5 from top to bottom, esterification reaction tower 5 upper inlet are located between bubble trap 5.1 flashers 5.2, esterification reaction tower 5 lower inlet are located at packing tower 5.4 belows, and packing tower 5.4 is the packing towers that are made of fiber, silk screen, Pall ring, conjugate ring, cascade ring and flat ring.
Embodiment 2:
Be with the difference of embodiment 1: packing tower 5.4 is the packing towers that are made of fiber.
Embodiment 3:
Be with the difference of embodiment 1: packing tower 5.4 is the packing towers that are made of silk screen.
Embodiment 4:
Be with the difference of embodiment 1: packing tower 5.4 is the packing towers that are made of Pall ring.
Embodiment 5:
Be with the difference of embodiment 1: packing tower 5.4 is the packing towers that are made of conjugate ring.
Embodiment 6:
Be with the difference of embodiment 1: packing tower 5.4 is the packing towers that are made of cascade ring.
Embodiment 7:
Be with the difference of embodiment 1: packing tower 5.4 is the packing towers that are made of flat ring.
Claims (9)
1. the continuous producing apparatus of a biofuel, comprise the biofuel reaction unit, connecting tube and ducted volume pump, transferpump and under meter, it is characterized in that: described biofuel reaction unit comprises mixing tank (2), well heater I (3), pipeline reactor I (4), esterification reaction tower (5), catalyst separator (10), methyl alcohol basin (9), rosaline flow container (12), pipeline reactor II (24), flashing tower (15), glycerin separator (16), distillation tower (17) and biofuel basin (19), mixing tank (2) outlet is connected with pipeline reactor I (4) by well heater I (3), pipeline reactor I (4) outlet conduit is connected with esterification reaction tower (5) upper inlet, and esterification reaction tower (5) outlet at bottom is communicated with catalyst separator (10); Described methyl alcohol basin (9) outlet is connected with rosaline flow container (12) import, rosaline flow container (12) outlet is connected 10 with catalyst separator) the outlet volume pump that passes through separately in top is connected with pipeline reactor II (24), pipeline reactor II (24) outlet conduit connects flashing tower (15) upper inlet, flashing tower (15) outlet at bottom pipeline connects glycerin separator (16) lower inlet, the outlet of glycerin separator (16) top connects distillation tower (17) bottom, and distillation tower (17) top exit is connected with biofuel basin (19).
2. the continuous producing apparatus of biofuel according to claim 1, it is characterized in that: be provided with spiral plate (30) in described pipeline reactor I, the II (4,24), spiral plate (30) is provided with the traverse baffle (31) that staggers mutually.
3. the continuous producing apparatus of biofuel according to claim 1, it is characterized in that: be provided with bubble trap (5.1), flasher (5.2), falling film evaporator (5.3) and packing tower (5.4) in the described esterification reaction tower (5) from top to bottom, described esterification reaction tower (5) upper inlet is located between bubble trap (5.1) and the flasher (5.2), and described esterification reaction tower (5) lower inlet is located at packing tower (5.4) below.
4. the continuous producing apparatus of biofuel according to claim 3, it is characterized in that: described packing tower (5.4) is by any one or a few packing tower that consists of (5.4) in fiber, silk screen, Pall ring, conjugate ring, cascade ring and the flat ring.
5. the continuous producing apparatus of each described biofuel according to claim 1 ~ 4, it is characterized in that: the continuous producing apparatus of described biofuel also comprises methanol recovery device, methanol recovery device comprises methanol rectifying tower (8) and condenser (11,13), methanol rectifying tower (8) lower inlet is connected with esterification reaction tower (5) top exit pipeline, methanol rectifying tower (8) top duct is provided with two outlets, an outlet is connected with esterification reaction tower (5) lower inlet through pipeline connection traffic meter I (6), another outlet is connected with methyl alcohol basin (9) import by condenser I (11) through pipeline connection traffic meter II (7) road, and another import of methyl alcohol basin (9) is connected with flashing tower (15) top exit by condenser II (13).
6. the continuous producing apparatus of each described biofuel according to claim 1 ~ 4 is characterized in that: be provided with well heater II (14) between described pipeline reactor II (24) and the flashing tower (15).
7. the continuous producing apparatus of each described biofuel according to claim 1 ~ 4 is characterized in that: be provided with condenser III (18) between described distillation tower (17) and the biofuel basin (19).
8. the continuous producing apparatus of each described biofuel according to claim 1 ~ 4 is characterized in that: described catalyst separator (10) outlet at bottom pipeline is connected with an acidic catalyst withdrawing can (27).
9. the continuous producing apparatus of each described biofuel according to claim 1 ~ 4 is characterized in that: described glycerin separator (16) outlet at bottom pipeline is connected with glycerine basin (21).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012205380268U CN202912929U (en) | 2013-02-18 | 2013-02-18 | Continuous production equipment for biodiesel |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012205380268U CN202912929U (en) | 2013-02-18 | 2013-02-18 | Continuous production equipment for biodiesel |
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| CN202912929U true CN202912929U (en) | 2013-05-01 |
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| CN2012205380268U Withdrawn - After Issue CN202912929U (en) | 2013-02-18 | 2013-02-18 | Continuous production equipment for biodiesel |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103031215A (en) * | 2013-02-18 | 2013-04-10 | 广西合众能源股份有限公司 | Continuous production device and method of biodiesel |
| CN104087412A (en) * | 2014-07-17 | 2014-10-08 | 李安民 | Process and equipment for fatty acid methyl ester refining |
| CN104830542A (en) * | 2015-04-23 | 2015-08-12 | 西安交通大学 | Device and method for continuous reduction of biodiesel acid value by compounding of supercritical methanol and catalyst |
| CN105670804A (en) * | 2016-03-22 | 2016-06-15 | 唐山金利海生物柴油股份有限公司 | Equipment and method for preparing biodiesel under low-temperature gas-phase methanol conditions |
| CN110172377A (en) * | 2019-06-20 | 2019-08-27 | 成都恒润高新科技股份有限公司 | A method of biodiesel is continuously prepared using waste animal and vegetable oil |
| CN112410128A (en) * | 2020-11-21 | 2021-02-26 | 贵州锦江生物能源科技有限公司 | Biodiesel continuous esterification production device |
| CN114634843A (en) * | 2022-04-07 | 2022-06-17 | 湖北天基生物能源科技发展有限公司 | Method for esterification reaction of swill-cooked dirty oil and subcritical gaseous methanol |
-
2013
- 2013-02-18 CN CN2012205380268U patent/CN202912929U/en not_active Withdrawn - After Issue
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103031215A (en) * | 2013-02-18 | 2013-04-10 | 广西合众能源股份有限公司 | Continuous production device and method of biodiesel |
| CN103031215B (en) * | 2013-02-18 | 2014-05-07 | 广西合众能源股份有限公司 | Continuous production device and method of biodiesel |
| CN104087412A (en) * | 2014-07-17 | 2014-10-08 | 李安民 | Process and equipment for fatty acid methyl ester refining |
| CN104830542A (en) * | 2015-04-23 | 2015-08-12 | 西安交通大学 | Device and method for continuous reduction of biodiesel acid value by compounding of supercritical methanol and catalyst |
| CN105670804A (en) * | 2016-03-22 | 2016-06-15 | 唐山金利海生物柴油股份有限公司 | Equipment and method for preparing biodiesel under low-temperature gas-phase methanol conditions |
| CN110172377A (en) * | 2019-06-20 | 2019-08-27 | 成都恒润高新科技股份有限公司 | A method of biodiesel is continuously prepared using waste animal and vegetable oil |
| CN112410128A (en) * | 2020-11-21 | 2021-02-26 | 贵州锦江生物能源科技有限公司 | Biodiesel continuous esterification production device |
| CN114634843A (en) * | 2022-04-07 | 2022-06-17 | 湖北天基生物能源科技发展有限公司 | Method for esterification reaction of swill-cooked dirty oil and subcritical gaseous methanol |
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