CN101020838A - Biodiesel oil preparing process and apparatus - Google Patents
Biodiesel oil preparing process and apparatus Download PDFInfo
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- CN101020838A CN101020838A CNA2007100676457A CN200710067645A CN101020838A CN 101020838 A CN101020838 A CN 101020838A CN A2007100676457 A CNA2007100676457 A CN A2007100676457A CN 200710067645 A CN200710067645 A CN 200710067645A CN 101020838 A CN101020838 A CN 101020838A
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- methyl alcohol
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Abstract
The present invention relates to biodiesel oil preparing process and apparatus. In the heated esterification reaction of methanol, concentrated sulfuric acid and material oil inside a stirring reactor, the methanol is first heated and gasified into methanol vapor before entering the reactor from the bottom, and this results in liquid phase-gas phase reaction with high reaction speed and short reaction period. Therefore, the present invention has the features of fast reaction speed, short reaction period, saving in material, lowered heat energy consumption and other advantages, and is suitable for preparing biodiesel oil with different kinds of material oil.
Description
Technical field
The present invention relates to a kind of preparation technology and device thereof of biofuel, particularly relate to methyl alcohol vapour phase system and reflux technique and device thereof in the biodiesel manufacture technology esterification, and methyl esters vapour phase continuous distillation process and device thereof.
Background technology
Biofuel mainly is to use chemical method production at present, promptly carries out transesterification with animal-plant oil and methyl alcohol under acid base catalysator and high temperature, generates corresponding fatty acid methyl ester, promptly gets biofuel through washing processing such as drying again.Its conventional production process of acid-catalyzed esterification reaction is raw materials pretreatment, removes raw material well cuts and dehydration, and esterification, separation, distillation, alcohol reclaim and purification processes, its esterification adds methyl alcohol and the vitriol oil and stock oil, heating in the stirring-type reactor, carry out esterification, most methods of fractional steps that adopt are carried out, and promptly react a stage, stop to stir, precipitated and separated, divide and to go by water-reducible dilute methanol, methyl alcohol that restock is new and sulfuric acid, being generally for three steps carries out.Another kind of production technique is the base catalysis esterification, and conventional production process is to utilize neutral grease and methyl alcohol under basic catalyst and heat effect, carries out transesterify.The weak point of above-mentioned two kinds of its existence of processing method is, the first, and above-mentioned two kinds of modes of production are various for separate equipment design, general acid-catalyzed esterification reaction is applicable to acidifying oil, economizes matter oil, waste oil etc.; And the base catalysis transesterification reaction requires acid value very low comparatively speaking, oil quality is required high, second, the common process esterification is the reaction between liquid phase and the liquid phase, grease is a liquid phase, methyl alcohol also is liquid phase, under the catalyzer existence condition, relies on molecular motion and mechanical stirring to impel the collision of oil molecule and methanol molecules, the power of molecular motion is limited, speed of response depends on restrictions such as mechanical property and sealing, and in the round shape reactor during stirring movement molecule rotate existing staticly relatively, greatly reduce the contact between the reactant molecule, speed of response is slow, long reaction time, and power consumption increase, raw material consumption is big; The 3rd, remove resultant water, long reaction time with the method for fractional steps in the common process; The 4th, the still-process energy consumption is big, and raw material consumption is big.
Summary of the invention
Its purpose of the present invention just is to provide a kind of preparation technology and device thereof of biofuel, have the shortening reaction times, improve output and quality, characteristics such as energy-conservation, and can in same equipment, realize two kinds of modes of production, be adapted to the grease production biofuel of various acid values.
The technical scheme that realizes above-mentioned purpose and take, comprise esterification, in the stirring-type reactor, add methyl alcohol and the vitriol oil and stock oil, heating, carry out esterification, replenish in the described esterification and enter or the methyl alcohol that enters in the reactor that refluxes is to enter in the reactor behind valve from the reactor bottom behind the methyl alcohol gas through methanol steam producer heat temperature raising.
Comprise raw materials pretreatment, remove raw material well cuts and dehydration, esterification is separated, distillation, and alcohol reclaims and glycerin treatment.
1) esterification, at first in the stirring-type reactor, add methyl alcohol, methyl alcohol and stock oil mass ratio are (0.2-0.4): 1, under agitation add the vitriol oil then, the vitriol oil and stock oil mass ratio are (0.007-0.009): 1, add at last through pretreated stock oil, stir heat temperature raising down, esterification begins, and when oily temperature rise after methyl alcohol water distillation going along with is finished in the reactor during to 100-110 ℃, begins this moment to give birth to the methyl alcohol gas that produces in the device with methanol steam, temperature is 65-75 ℃, mend or be back in the reactor through valve from the reactor bottom, pump around circuit finishes until esterification;
2, transesterification reaction adds sodium methoxide solution, heat temperature raising in reactor, to 75-80 ℃, with the methyl alcohol gas that produces in the methanol steam producer, temperature is 65-75 ℃, mend or be back in the reactor through valve from the reactor bottom, pump around circuit finishes until transesterification reaction;
3, methyl ester distilled, the thick methyl esters after the washing dehydration is sent into methyl esters vapour phase producer internal heating heat up behind interchanger, to 130-180 ℃, enter in the methyl ester distilled still with methyl esters vapour phase tangent line again and realize flash distillation.Methyl ester distilled still methyl esters vapour outlet connects interchanger, obtains smart methyl esters, methyl ester distilled finishing after the exchanger heat exchange.
Compared with prior art the present invention has the following advantages,
1, because the present invention has adopted the design cycle of two kinds of production technique, thereby can finish two kinds of technological process of productions in same apparatus and process, be applicable to the grease inferior of various lipid acid, it is strong to have suitability, and technology is simple, convenience operation;
2, design band water distil process owing in the technological design of the present invention, thereby shortened the reaction times greatly, improved output.
3, because having designed vapour phase, the present invention mends methanol technics, become liquid phase and liquid phase reaction and be liquid phase and vapour-phase reaction, adopt the methyl alcohol vapour phase to enter oil phase from still pucking bubble, and equally under churned mechanically booster action, make the abundant touch-safe of oil molecule and methanol molecules, thereby improved speed of response greatly, have short characteristics of reaction times.
4, because the methyl ester distilled methyl esters vapour phase that adopted of the present invention is advanced the design of still distillatory continuously, utilize the vapour phase methyl esters to come condensation methyl esters steam, use the cold thick methyl esters of methyl esters steam heating conversely, thereby improved distillation speed greatly, it is short to have distillation time, reduce the finished product color and luster, improve the quality of products and the characteristics of energy-saving and water-saving.
Description of drawings
Below in conjunction with drawings and Examples invention is further described.
Fig. 1 is a technical process functional block diagram of the present invention;
Fig. 2 mends methanol loop production technology principle synoptic diagram for the methyl alcohol vapor phase catalytic;
Fig. 3 is a methanol steam generator apparatus principle schematic;
Fig. 4 is a methyl alcohol vapour phase distil process principle schematic.
Specific embodiments
Its technological principle of the present invention adopts the methyl alcohol vapour phase to enter oil phase from bottom bubbling mode, and under churned mechanically booster action, oil molecule is fully contacted with methanol molecules join, and has accelerated speed of response greatly.
Its technology comprises esterification, in stirring-type reactor 1, add methyl alcohol and the vitriol oil and stock oil, heating, carry out esterification, its technical process replenishes in the described esterification and enters or the methyl alcohol that enters in the reactor 1 that refluxes is to enter in the reactor 1 behind valve 7 from reactor 1 bottom behind the methyl alcohol gas through methanol steam producer 2 heat temperature raisings as shown in Figure 2.
Its technological process device as shown in Figure 2, comprise stirring-type reactor 1, Methanol Recovery device 6, qualified methyl alcohol receiver 4 and methanol pump 5 and methyl alcohol under meter 3, also comprise methanol steam producer 2, methanol steam producer 2 import C are connected qualified methyl alcohol receiver 4 after methyl alcohol under meter 3 and methanol pump 5, methanol steam producer 2 outlet d are connected to reactor 1 bottom methanol eddy mouth through valve 7.
Described methanol steam producer 2 comprises cylindrical shell 11 and is installed in heat transfer tube 10 in the housing 11 and the tube sheet 9 at housing 11 two ends, as shown in Figure 3, last lower tubesheet 9 connects raises the nose above water to breathe to constitute respectively sweating room 8 and feed chamber 12, housing 11 upper side perforate a connect the heating steam import, and housing 11 lower side perforates 6 connect vapour outlet.
Workflow is, earlier the methanol solution that measures is squeezed in the reactor 1, open reactor 1 agitator, reactor 1 adds the vitriol oil under agitation condition, and then the stock oil of water has been taken off in adding, reinforced finishing, open the heating valve on the reactor 1, in the reactor 1 during oily temperature rise to 105 ℃ in the reactor 1 methyl alcohol water distillation going along with evaporate basically, and through Methanol Recovery device 6 recovery methyl alcohol, at this moment, open methanol pump 5, enter methyl alcohol through methyl alcohol under meter 3 methyl alcohol and enter in the methanol steam producer 2, open the heating valve, methyl alcohol is at methanol steam producer 2 internal heating to 70 ℃, and methanol steam enters in the reactor 1 from reactor 1 bottom through valve 7, finishes until reaction.
From 5000 liter reactors is example, and the time of mending methyl alcohol is 1 hour, and the amount of mending methyl alcohol is 1000kg, and reaction is finished, and acid value drops to 1.9mg/g.
When stock oil is lower crude oil of acid value or refining oil, its technical process as shown in Figure 1, through pre-treatment, transesterify separates, and after glycerin treatment and the distillation, finishes the preparation of biofuel.
When stock oil is the higher waste oil of acid value, its technical process as shown in Figure 1, through esterification, transesterify separates, and after glycerin treatment and the distillation, finishes the preparation of biofuel.
Its technological process comprises raw materials pretreatment, removes raw material well cuts and dehydration, and esterification is separated, distillation, and alcohol reclaims and glycerin treatment, as shown in Figure 1, 2.
1) esterification, at first in stirring-type reactor 1, add methyl alcohol, methyl alcohol and stock oil mass ratio are (0.2-0.4): 1, under agitation add the vitriol oil then, the vitriol oil and stock oil mass ratio are (0.007-0.009): 1, add at last through pretreated stock oil, stir heat temperature raising down, esterification should begin, and when oily temperature rise after methyl alcohol water distillation going along with is finished in the reactor during to 100-110 ℃, begins the methyl alcohol gas that produces with in the methanol steam producer 2 this moment, temperature is 65-75 ℃, mend or be back in the reactor 1 from reactor 1 bottom through valve 7, pump around circuit finishes until esterification;
2) transesterification reaction adds sodium methoxide solution, heat temperature raising in reactor 1, to 75-80 ℃, with the methyl alcohol gas that produces in the methanol steam producer 2, temperature is 65-75 ℃, mend or be back in the reactor 1 from reactor 1 bottom through valve 7, pump around circuit finishes until transesterification reaction;
3) methyl ester distilled, thick methyl esters after the washing dehydration is sent into methyl esters vapour phase producer 13 internal heating behind parallel operation 15 heat up, to 130-180 ℃, enter methyl ester distilled still 14 internal heating with methyl esters vapour phase tangent line again, methyl ester distilled still 14 methyl esters vapour outlets connect interchanger 15, after interchanger 15 heat exchanges, obtain smart methyl esters, methyl ester distilled finishing.
Its device also comprises methyl ester distilled still 14, as shown in Figure 4, methyl ester distilled still 14 top vapour outlet k connect interchanger 15 top shell side import e, interchanger 15 bottom shell side outlets connect smart methyl esters outlet f, interchanger 15 tube side lower ends are thick methyl esters import h, interchanger 15 tube side upper steam outlet j connects methyl esters vapour phase producer 13 import p, 13 outlets of methyl esters vapour phase producer connect methyl ester distilled still 14 opening for feed m, described methyl ester distilled still 14 opening for feed m are arranged on still kettle cylindrical shell upper side, and are the cylindrical shell tangential direction.
Utilize 60 ℃ of cold thick methyl esters to come the methyl esters steam of 180 ℃ of condensations, use 60 ℃ of cold thick methyl esters of methyl esters steam heating of 180 ℃ conversely, energy-saving and water-saving.And thick methyl esters vapour phase tangent line has been accelerated distillation speed greatly by still.
No matter what grease inferior is acid value be, remove well cuts inferior through pre-treatment (washing), dehydration, esterification makes the lipid acid that dissociates in the oil become fatty acid methyl ester earlier.Esterification is specially earlier the methyl alcohol that measures, the mass ratio of quantity of methyl alcohol and oil mass is 0.3: 1, under agitation add sulfuric acid in the reactor again, the vitriol oil is 0.008: 1 with the mass ratio of oil, add the province's matter oil that has taken off water at last, under agitation heat up 60 ℃ and begin reaction, when the water distillation going along with of oily temperature rise to 105 ℃ original methyl alcohol all evaporates basically, so in time, begin to inject from reactor bottom bubbling with the methyl alcohol gas that produces in the methanol steam producer (the gas temperature is at 64.5-70 ℃), the good control of amount should anti-still be example with the methyl alcohol under meter with 5000 liters, the methyl alcohol flow control is at 2501/h, time is about 3 hours, specifically be as the criterion,, illustrate that esterification finishes when acid value drops to below 2.5 to survey acid value.Enter the transesterify stage, the sodium methoxide solution for preparing is in advance added in the reactor, part Na ion and the original H that adds in the sodium methylate
2S0
4With become to give birth to Na
2SO
4And less water, under 75-80 ℃, methanol loop backflow 2-3 hour is surveyed below the acid value to 2.5 at last, illustrates that being reflected in the reactor of two stages all finish.Separation, glycerin treatment, the methyl esters washing, alcohol recovery etc., enter methyl ester distilled at last, with the thick methyl esters after the washing dehydration, enter interchanger, the methyl esters temperature is raised to about 120 ℃, enters methyl esters vapour phase producer again, make methanol temperature rise to boiling point, because of mixed methyl is just boiled under 5mm mercury column vacuum 130 ℃, 180 ℃ of full boiling points enter methyl ester distilled still with the vapour phase tangent line, and its distillation speed advances the speed of still considerably beyond the liquid phase of routine, because the time compole that methyl esters stops is short, thereby produce the excellent as edible salad oil in pool in still.
Claims (6)
1, a kind of preparation technology of biofuel, comprise esterification, in stirring-type reactor (1), add methyl alcohol and the vitriol oil and stock oil, heating, carry out esterification, it is characterized in that, replenish in the described esterification and enter or the methyl alcohol that enters in the reactor (1) that refluxes is to enter in the reactor (1) behind valve (7) from reactor (1) bottom behind the methyl alcohol gas through methanol steam producer (2) heat temperature raising.
2, a kind of preparation technology of biofuel comprises raw materials pretreatment, removes raw material well cuts and dehydration, and esterification is separated, distillation, and alcohol reclaims and glycerin treatment, it is characterized in that:
1) esterification, at first in stirring-type reactor (1), add methyl alcohol, methyl alcohol and raw material are (0.2-0.4) by mass ratio: 1, under agitation add the vitriol oil then, the vitriol oil and stock oil mass ratio are (0.007-0.009): 1, add at last through pretreated stock oil, stir heat temperature raising down, esterification begins, and when oily temperature rise after methyl alcohol water distillation going along with is finished in the reactor during to 100-110 ℃, begins the methyl alcohol gas that produces with in the methanol steam producer (2) this moment, temperature is 65-75 ℃, mend or be back in the reactor (1) through valve (7) from reactor (1) bottom, pump around circuit finishes until esterification;
2) transesterification reaction, in reactor (1), add sodium methoxide solution, heat temperature raising, to 75-80 ℃, with the methyl alcohol gas that produces in the methanol steam producer (2), temperature is 65-75 ℃, mends or is back in the reactor (1) through valve (7) from reactor (1) bottom, pump around circuit finishes until transesterification reaction;
3) methyl ester distilled, thick methyl esters after the washing dehydration is sent into methyl esters vapour phase producer (13) internal heating behind interchanger (15) heat up, to 130-180 ℃, enter methyl ester distilled still (14) internal heating with methyl esters vapour phase tangent line again, methyl ester distilled still methyl esters vapour outlet connects interchanger (15), after heat exchange (15) heat exchange, obtain smart methyl esters, methyl ester distilled finishing.Reduce the boiling point of mixed methyl, still kettle is worked under 3mm mercury column residual voltage, and methyl esters steam is gone into still in the flash distillation mode.
3, the device of a kind of biodiesel manufacture technology according to claim 1 and 2, comprise stirring-type reactor (1), Methanol Recovery device (6), qualified methyl alcohol receiver (4) and methanol pump (5) and methyl alcohol under meter (3) is characterized in that, also comprise methanol steam producer (2).Methanol steam producer (2) import (c) is connected qualified methyl alcohol receiver (4) after methyl alcohol under meter (3) and methanol pump (5), methanol steam producer (2) outlet (d) is connected to reactor (1) bottom methanol eddy mouth through valve (7).
4, the device of a kind of biodiesel manufacture technology according to claim 1 and 2, it is characterized in that, described methanol steam producer (2) comprises cylindrical shell (11) and is installed in the interior heat transfer tube (10) of housing (11) and the tube sheet (9) at housing (11) two ends, last lower tubesheet (9) connects raises the nose above water to breathe to constitute respectively sweating room (8) and feed chamber (12), housing (11) upper side perforate (a) connects the heating steam import, and housing (11) lower side perforate (6) connects vapour outlet.
5, the device of a kind of biodiesel manufacture technology according to claim 2, comprise methyl alcohol still kettle (14), it is characterized in that, methyl ester distilled still (14) top vapour outlet (k) connects interchanger (15) top shell side import (e), the shell side outlet of interchanger (15) bottom connects smart methyl esters outlet (f), interchanger (15) tube side lower end is thick methyl esters import (h), interchanger (15) tube side upper steam outlet (j) connects methyl esters vapour phase producer (13) import (9), and methyl esters vapour phase producer (13) outlet (n) connects methyl ester distilled still (14) opening for feed (m).
6, the device of a kind of biodiesel manufacture technology according to claim 5 is characterized in that, described methyl ester distilled still (14) opening for feed (m) is arranged on still kettle cylindrical shell upper side, and is the cylindrical shell tangential direction.
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| Application Number | Priority Date | Filing Date | Title |
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| CNA2007100676457A CN101020838A (en) | 2007-03-23 | 2007-03-23 | Biodiesel oil preparing process and apparatus |
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| CNA2007100676457A CN101020838A (en) | 2007-03-23 | 2007-03-23 | Biodiesel oil preparing process and apparatus |
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101654624A (en) * | 2008-08-21 | 2010-02-24 | 庞汝瑞 | Gaseous phase circulation production method for biodiesel and device therefor |
| CN101974370A (en) * | 2010-09-28 | 2011-02-16 | 上海绿铭环保科技股份有限公司 | Heat exchange system for industrialized production of biodiesel |
| CN101294097B (en) * | 2008-06-19 | 2011-07-06 | 蔡志武 | Multifunctional reaction still for preparing biological diesel oil and operation method thereof |
| CN102311883A (en) * | 2011-08-10 | 2012-01-11 | 北京清研利华石油化学技术有限公司 | Method for preparing high-purity biodiesel |
| CN103320233A (en) * | 2013-07-16 | 2013-09-25 | 唐山金利海生物柴油股份有限公司 | Preparation method of biodiesel |
| CN103897809A (en) * | 2012-12-27 | 2014-07-02 | 福建大青实业有限公司 | Processing technology of soapberry biodiesel |
| CN104087412A (en) * | 2014-07-17 | 2014-10-08 | 李安民 | Process and equipment for fatty acid methyl ester refining |
| CN104403804A (en) * | 2013-12-11 | 2015-03-11 | 宁波杰森绿色能源科技有限公司 | Method for removing methanol from crude methyl ester |
| CN104402715A (en) * | 2013-12-11 | 2015-03-11 | 宁波杰森绿色能源科技有限公司 | Method for removing low-boiling-point substances from crude methyl ester |
| CN111234934A (en) * | 2020-03-23 | 2020-06-05 | 龙岩卓越新能源股份有限公司 | Method for producing biodiesel by continuous ester exchange of waste oil |
| CN114164052A (en) * | 2021-11-30 | 2022-03-11 | 安徽三联学院 | Production process and equipment of low-sulfur-content biodiesel |
| CN114214121A (en) * | 2021-12-14 | 2022-03-22 | 浙江东江能源科技有限公司 | High-quality low-sulfur-content biodiesel preparation device and preparation method |
-
2007
- 2007-03-23 CN CNA2007100676457A patent/CN101020838A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101294097B (en) * | 2008-06-19 | 2011-07-06 | 蔡志武 | Multifunctional reaction still for preparing biological diesel oil and operation method thereof |
| CN101654624A (en) * | 2008-08-21 | 2010-02-24 | 庞汝瑞 | Gaseous phase circulation production method for biodiesel and device therefor |
| CN101974370A (en) * | 2010-09-28 | 2011-02-16 | 上海绿铭环保科技股份有限公司 | Heat exchange system for industrialized production of biodiesel |
| EP2743336A4 (en) * | 2011-08-10 | 2015-04-22 | Beijing Qingyanlihua Petroleum Chemistry Co Ltd | Method for preparing high purity biodiesel |
| CN102311883A (en) * | 2011-08-10 | 2012-01-11 | 北京清研利华石油化学技术有限公司 | Method for preparing high-purity biodiesel |
| WO2013020514A1 (en) * | 2011-08-10 | 2013-02-14 | 北京清研利华石油化学技术有限公司 | Method for preparing high purity biodiesel |
| CN102311883B (en) * | 2011-08-10 | 2013-04-24 | 北京清研利华石油化学技术有限公司 | Method for preparing high-purity biodiesel |
| US9145527B2 (en) | 2011-08-10 | 2015-09-29 | Beijing Qingyanlihua Petroleum Chemistry Co., Ltd. | Method for preparing high purity biodiesel |
| EP2743336A1 (en) * | 2011-08-10 | 2014-06-18 | Beijing Qingyanlihua Petroleum Chemistry Co., Ltd. | Method for preparing high purity biodiesel |
| CN103897809A (en) * | 2012-12-27 | 2014-07-02 | 福建大青实业有限公司 | Processing technology of soapberry biodiesel |
| CN103320233B (en) * | 2013-07-16 | 2014-08-06 | 唐山金利海生物柴油股份有限公司 | Preparation method of biodiesel |
| CN103320233A (en) * | 2013-07-16 | 2013-09-25 | 唐山金利海生物柴油股份有限公司 | Preparation method of biodiesel |
| CN104403804A (en) * | 2013-12-11 | 2015-03-11 | 宁波杰森绿色能源科技有限公司 | Method for removing methanol from crude methyl ester |
| CN104402715A (en) * | 2013-12-11 | 2015-03-11 | 宁波杰森绿色能源科技有限公司 | Method for removing low-boiling-point substances from crude methyl ester |
| CN104087412A (en) * | 2014-07-17 | 2014-10-08 | 李安民 | Process and equipment for fatty acid methyl ester refining |
| CN111234934A (en) * | 2020-03-23 | 2020-06-05 | 龙岩卓越新能源股份有限公司 | Method for producing biodiesel by continuous ester exchange of waste oil |
| CN114164052A (en) * | 2021-11-30 | 2022-03-11 | 安徽三联学院 | Production process and equipment of low-sulfur-content biodiesel |
| CN114214121A (en) * | 2021-12-14 | 2022-03-22 | 浙江东江能源科技有限公司 | High-quality low-sulfur-content biodiesel preparation device and preparation method |
| CN114214121B (en) * | 2021-12-14 | 2024-02-20 | 浙江东江能源科技有限公司 | Preparation device and preparation method of high-quality low-sulfur biodiesel |
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Application publication date: 20070822 |