CN106190591A - The esterification of a kind of biodiesel, ester exchange reaction method - Google Patents
The esterification of a kind of biodiesel, ester exchange reaction method Download PDFInfo
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- CN106190591A CN106190591A CN201510536907.4A CN201510536907A CN106190591A CN 106190591 A CN106190591 A CN 106190591A CN 201510536907 A CN201510536907 A CN 201510536907A CN 106190591 A CN106190591 A CN 106190591A
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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
Abstract
The invention discloses the esterification of a kind of biodiesel, ester exchange reaction method, it is characterized in that: methanol is after methanol gasifying device is heated, pressurizeed, gasification temperature is 84 DEG C～220 DEG C, pressure is 0.2MPa～5.5MPa, making methanol be in nearly subcritical state, methanol gas uses porous type pipeline to inject in reaction tower with this state bottom reaction tower；Raw oil material is preheating to 80 DEG C～120 DEG C by heater, is then sprayed onto in reaction tower with certain flow rate from reaction tower top；The temperature kept and control in reaction tower is 84 DEG C～220 DEG C, pressure is 0.2MPa～5.5MPa, and methanol is in subcritical state under this temperature and pressure, raw oil material and methanol dissolve each other, making two alternate chemical reactions under the conditions of popular response become single-phase chemical reaction, solve interphase mass transfer problem, response speed is fast, esterification, ester exchange efficiency height, without adding catalyst in course of reaction.
Description
Technical field
The invention belongs to the production technical field of biodiesel, in particular it relates to the esterification of a kind of biodiesel,
Ester exchange reaction method.
Background technology
Biodiesel refers to the fat obtained through ester exchange reaction by animal and plant fat with alcohol (methanol or ethanol)
Acid mono alkyl ester, most typically fatty acid methyl ester.Compared with traditional fossil energy, its sulfur and aromatic hydrocarbons contain
Measure low, flash-point is high, Cetane number is high, have good lubricity, can partly add in petrifaction diesel,
Thus biodiesel is a kind of real green diesel.
At present, the method for industrialized production biodiesel has chemical synthesis and enzyme synthetic method, biological bavin
The chemical synthesis of oil is to use oils and fats and the low-carbon alcohols such as methanol or ethanol, and uses acidity or base catalysis
There is esterification or ester exchange reaction in agent, generates corresponding fatty acid methyl ester or ethyl ester, more scrubbed is drying to obtain
Biodiesel.Methanol or ethanol can be recycled in process of production, produce about 10% in production process
Side-product glycerol.But chemical method biodiesel synthesis has the disadvantage that: reaction temperature is higher, complex process；
Using the methanol of excess in course of reaction, subsequent technique must have corresponding alcohol retracting device, and processing procedure is numerous
Multiple, energy consumption height；Water and free fatty in glyceride stock can have a strong impact on bio-diesel yield and quality；
Purifying products is complicated, and esterification products is difficult to reclaim；Reaction generate by-product be difficult to remove, and use acid,
Base catalyst produces substantial amounts of waste water, and environment is easily caused secondary pollution etc. by the discharge of spent acid, alkali liquor.Due to
Biological enzyme biodiesel synthesis is utilized to have reaction condition gentleness, little, the non-pollutant discharge of alcohol consumption etc. excellent
Point, has environment friendly, thus is increasingly subject to the attention of people.But utilize the biological bavin of biological enzyme preparation
Oil presently, there are some problem demanding prompt solutions: lipase to the esterification of long-chain fatty alcohol or transesterification effectively,
And low to short chain fatty alcohol (such as methanol or ethanol etc.) conversion ratio, it is typically only 40%～60%；Methanol and second
Alcohol has certain toxicity to enzyme, easily makes enzyme inactivate；By-product glycerin and shipwreck are to reclaim, not only to product
Formed consistent, and glycerol is also toxic to enzyme；The existence of short chain fatty alcohol and glycerol all affects the reaction of enzyme
Activity and stabill, makes be greatly shortened the service life of solidification enzyme.So biological enzyme industrialized production is biological
Diesel oil there is also many problems.
Such as, patent documentation CN1718679 discloses a kind of subcritical methanol phase solid acid alkali catalytic stearic
The method of exchange system biodiesel, although the method has reaction temperature and pressure is low, equipment investment is little, instead
Advantage short between Ying Shi, but this inventive method must use solid catalyst to realize, and comes from production cost
Saying, the use cost of solid catalyst is higher.It addition, this inventive method have employed autoclave reactive mode,
Belong to intermittent reaction, compared with tower reactor, be not suitable for the production of serialization.
Patent documentation CN101921631A discloses the production method of biological bavin, although also use gas phase first
Alcohol reacts under the effect of catalyst with oils and fats, but methanol is not in subcritical state, response speed
Relatively slow, reaction is not thorough, must add the compositions of potassium hydroxide and accelerator as instead in course of reaction
Catalyst, reaction is answered to need the subsequent treatment to catalyst after terminating.
Patent documentation CN1473907 discloses a kind of method producing biological bavin, to raw oil material pretreatment
Require higher, first need raw oil material is used vacuum dehydration, esterification reaction process is used pump forced circulation,
Easily cause esterifier material coking, course of reaction is added the catalyst of higher proportion to equipment corrosion
Property is higher, and whole reaction process is cumbersome.
Patent documentation CN102586032A discloses the production method of a kind of biological bavin, first to bio-oil
Carry out pretreatment, use filtration, aquation degumming, adsorption bleaching, solvent method dewaxing process by biomass starting material
Oil refiner becomes the mixture of the triglyceride that no color or smell is transparent；The fatty acid ester that carbon chain lengths is different
Produce；Fatty acid ester addition vaporizer carries out separated purification of reducing pressure.This inventive method is to raw oil material
Take a series of oil and fat refining means, as the pretreatment process such as aquation degumming, solvent method dewaxing can be to ring
Certain pollution is caused in border, and higher to the requirement of raw material in course of reaction, and complex manufacturing produces energy
Consumption height.
Patent documentation CN101812375A discloses the life of the self-catalytic esterification of a kind of biodiesel, ester exchange
Product method, it is characterised in that comprise the following steps: by raw oil that acid number is 50～200mgKOH/g and alcohol
Put in proportion in autoclave, at 3～10MPa pressure be to react 9～28 under 200～280 DEG C of temperature conditionss
Hour, i.e. prepare biodiesel oil product.This inventive method has certain restriction to raw oil material acid value,
Be not suitable for the raw oil material of acid number ＜ 50mgKOH/g, and reaction pressure and temperature higher, the response time
Longer.
Patent documentation CN1760335 discloses a kind of preparing biological diesel oil by esterifying, ester interchanging greases in high acid number
Method, it is characterised in that comprise the steps: (1), by high-acid value grease and methanol with volume ratio 100:
The ratio of 50～200 adds autoclave, adds oils and fats weight 0.5～the lewis acid catalyst of 5%, controls anti-
Answer temperature 160～220 DEG C, reaction pressure 1～8MPa, response time 5～50 minutes；(2), reaction terminates
After product separated methanol that (1) is obtained, centrifugal or filter to isolate partial catalyst, water elution removes
Residual glycerine and catalyst, be refining to obtain biodiesel.This inventive method is applicable to high-acid-value material oils and fats,
And must be added to acidic catalyst and could meet reaction condition, reaction subsequent handling is loaded down with trivial details, needs catalysis
Centrifugal or the filtration separating treatment of agent.
Summary of the invention
Present invention aims to the defect of above-mentioned existence and provide the esterification of a kind of biodiesel, ester to hand over
Change reaction method.The inventive method has a characteristic that (1) production technology is simple, can realize continuous metaplasia
Producing, energy consumption is low, instead of traditional reactor stirring reactive mode；(2) reaction mass is at reaction tower
The internal stops time is short, is swift in response, and reaction efficiency is high, and homogeneous heating is difficult to coking；(3) need not right
Raw oil material carries out pretreatment.(4) under nearly subcritical state, raw oil material and methanol dissolve each other, and make
Two alternate chemical reactions under the conditions of popular response become single-phase chemical reaction, solve interphase mass transfer problem,
Response speed is fast, esterification, ester exchange reaction efficiency height, and methanol polarity in this case is relatively strong, can be certainly
Body is as esterification, the catalyst of ester exchange reaction, without adding catalyst in course of reaction.
For reaching above-mentioned purpose, the present invention provides the esterification of a kind of biodiesel, ester exchange reaction method, bag
Include following steps:
(1) methanol is after methanol gasifying device is heated, pressurizeed, and gasification temperature is 84 DEG C～220 DEG C, pressure
For 0.2MPa～5.5MPa, making methanol be in nearly subcritical state, methanol gas uses porous type pipeline from instead
Tower bottom is answered to inject in reaction tower with this state；Methanol need to heat through methanol gasifying device, pressurize after reach one
Plant nearly precritical state and could meet the reaction condition of the method；
(2) raw oil material is preheating to 80 DEG C～120 DEG C by heater, then from reaction tower top with necessarily
Flow velocity is sprayed onto in reaction tower, and gaseous methanol the most inversely interts with the oils and fats drop landed during ascension；
(3) keeping and the temperature that controls in reaction tower is 84 DEG C～220 DEG C, pressure is 0.2MPa～5.5MPa,
And methanol is in subcritical state under this temperature and pressure, methanol and oils and fats dissolve each other, two interphase mass transfers
The rapidest abundant；
(4) for extending raw oil material and methanol time of contact and response time, reaction tower is perpendicular to oils and fats
Landing direction equidistant parallel arranges 3～9 blocks of sieve traies；
(5) every block of sieve tray is provided with Pressure gauge and liquidometer, observes every layer of sieve tray by Pressure gauge
Between pressure, observe, by liquidometer, the thickness that glyceride stock is piled up on sieve tray；Further, pass through
The size in aperture, sieve tray percent opening and UNICOM's sieve aperture on the charging rate of raw oil material, sieve tray
The control valve of column plate both sides adjusts sieve tray and piles up the thickness of oil layer；
(6) excessive methanol enters methanol distillation column from reaction tower top exit, then enters back into methanol gasifying device
Heat, pressurize after enter reaction tower recycle；
(7), after reaction terminates, bottom reaction tower, coarse biodiesel and the mixture of crude glycerine are discharged, subsequently
Enter the operations such as follow-up glycerol separation, biodiesel refining.
Further, the charging rate of raw oil material is 30L/min～100L/min.
Further, on sieve tray, the size in aperture is 10mm～50mm.
Further, sieve tray percent opening controls 5%～10%.
Further, the control thickness that on sieve tray, oils and fats is piled up is generally 10mm～100mm.
Detailed description of the invention
Following example are used for technical scheme is described, it is simple to be better understood from the present invention, but this
Bright application is not only limited to the scope of embodiment.
Embodiment 1:
Specific as follows: (1) methanol adds gentleness through methanol gasifying device and is pressurized to 84 DEG C, and 0.2MPa, from reaction tower
Bottom is injected in reaction tower with diffusion type；(2) glyceride stock is preheated to 80 DEG C from reaction tower top with 30L/min
Flow velocity be sprayed onto in reaction tower, keeping temperature in reaction tower tower is 84 DEG C, and pressure is 0.2MPa；(3) hang down
Directly arranging 3 blocks of sieve traies in oils and fats landing direction equidistant parallel, on column plate, screen-aperture size is 10mm,
Sieve tray percent opening is 5%；(4) monitored the pressure of every layer of sieve tray by Pressure gauge, regulation controls sieve
The thickness that on hole column plate, oils and fats is piled up is 10mm；(5) excessive methanol returns from reaction tower top exit entrance methanol
Receive tower, then enter back into methanol gasifying device heat, pressurize after enter reaction tower recycle；(6) reaction knot
Shu Hou, discharges coarse biodiesel and the mixture of crude glycerine bottom reaction tower, subsequently enters follow-up glycerol
The operations such as separation, biodiesel refining.Esterification, ester exchange reaction efficiency are 85.3%.
Embodiment 2:
Specific as follows: (1) methanol adds gentleness through methanol gasifying device and is pressurized to 112.5 DEG C, and 0.5MPa, from reaction
Tower bottom injects in reaction tower with diffusion type；(2) glyceride stock be preheated to 100 DEG C from reaction tower top with
The flow velocity of 65L/min is sprayed onto in reaction tower, and in holding reaction tower, temperature is 112.5 DEG C, and pressure is 0.5MPa；
(3) being perpendicular to oils and fats landing direction equidistant parallel and arrange 6 blocks of sieve traies, on column plate, screen-aperture size is
30mm, sieve tray percent opening is 7.5%；(4) monitored the pressure of every layer of sieve tray by Pressure gauge, adjust
It is 50mm that joint controls the thickness that on sieve tray, oils and fats is piled up；(5) excessive methanol enters from reaction tower top exit
Enter methanol distillation column, then enter back into methanol gasifying device heat, pressurize after enter reaction tower recycle；(6)
After reaction terminates, bottom reaction tower, discharge coarse biodiesel and the mixture of crude glycerine, subsequently enter follow-up
Glycerol separation, the operation such as biodiesel refining.Esterification, ester exchange reaction efficiency are 88.8%.
Embodiment 3
Specific as follows: (1) methanol adds gentleness through methanol gasifying device and is pressurized to 138 DEG C, and 1.0MPa, from reaction tower
Bottom is injected in reaction tower with diffusion type；(2) glyceride stock be preheated to 120 DEG C from reaction tower top with
The flow velocity of 100L/min is sprayed onto in reaction tower, keeps temperature 138 DEG C in reaction tower, pressure 1.0MPa；(3)
Being perpendicular to oils and fats landing direction equidistant parallel and arrange 9 blocks of sieve traies, on column plate, screen-aperture size is
50mm, sieve tray percent opening is 10%；(4) monitored the pressure of every layer of sieve tray by Pressure gauge, adjust
It is 90mm that joint controls the thickness that on sieve tray, oils and fats is piled up；(5) excessive methanol enters from reaction tower top exit
Enter methanol distillation column, then enter back into methanol gasifying device heat, pressurize after enter reaction tower recycle；(6)
After reaction terminates, bottom reaction tower, discharge coarse biodiesel and the mixture of crude glycerine, subsequently enter follow-up
Glycerol separation, the operation such as biodiesel refining.Esterification, ester exchange reaction efficiency are 96.0%.
Embodiment 4:
Specific as follows: (1) methanol adds gentleness through methanol gasifying device and is pressurized to 167 DEG C, and 2.0MPa, from reaction tower
Bottom is injected in reaction tower with diffusion type；(2) glyceride stock is preheated to 80 DEG C from reaction tower top with 30L/min
Flow velocity be sprayed onto in reaction tower, keeping temperature in reaction tower is 167 DEG C, and pressure is 2.0MPa；(3) hang down
Directly arranging 5 blocks of sieve traies in oils and fats landing direction equidistant parallel, on column plate, screen-aperture size is 20mm,
Sieve tray percent opening is 5%；(4) monitored the pressure of every layer of sieve tray by Pressure gauge, regulation controls sieve
The thickness that on hole column plate, oils and fats is piled up is 20mm；(5) excessive methanol returns from reaction tower top exit entrance methanol
Receive tower, then enter back into methanol gasifying device heat, pressurize after enter reaction tower recycle；(6) reaction knot
Shu Hou, discharges coarse biodiesel and the mixture of crude glycerine bottom reaction tower, subsequently enters follow-up glycerol
The operations such as separation, biodiesel refining.Esterification, ester exchange reaction efficiency are 96.7%.
Embodiment 5:
Specific as follows: (1) methanol adds gentleness through methanol gasifying device and is pressurized to 186.5 DEG C, and 3.0MPa, from reaction
Tower bottom injects in reaction tower with diffusion type；(2) glyceride stock be preheated to 100 DEG C from reaction tower top with
The flow velocity of 30L/min is sprayed onto in reaction tower, and in holding reaction tower, temperature is 186.5 DEG C, and pressure is 3.0MPa；
(3) being perpendicular to oils and fats landing direction equidistant parallel and arrange 6 blocks of sieve traies, on column plate, screen-aperture size is
30mm, sieve tray percent opening is 7.0%；(4) monitored the pressure of every layer of sieve tray by Pressure gauge, adjust
It is 50mm that joint controls the thickness that on sieve tray, oils and fats is piled up；(5) excessive methanol enters from reaction tower top exit
Enter methanol distillation column, then enter back into methanol gasifying device heat, pressurize after enter reaction tower recycle；(6)
After reaction terminates, bottom reaction tower, discharge coarse biodiesel and the mixture of crude glycerine, subsequently enter follow-up
Glycerol separation, the operation such as biodiesel refining.Esterification, ester exchange reaction efficiency are 97.8%.
Embodiment 6:
Specific as follows: (1) methanol adds gentleness through methanol gasifying device and is pressurized to 203.5 DEG C, and 4.0MPa, from reaction
Tower bottom injects in reaction tower with diffusion type；(2) glyceride stock be preheated to 120 DEG C from reaction tower top with
The flow velocity of 100L/min is sprayed onto in reaction tower, keeps temperature 203.5 DEG C in reaction tower, pressure 4.0MPa；(3)
Being perpendicular to oils and fats landing direction equidistant parallel and arrange 8 blocks of sieve traies, on column plate, screen-aperture size is
50mm, sieve tray percent opening is 10%；(4) monitored the pressure of every layer of sieve tray by Pressure gauge, adjust
It is 100mm that joint controls the thickness that on sieve tray, oils and fats is piled up；(5) excessive methanol is from reaction tower top exit
Enter methanol distillation column, then enter back into methanol gasifying device heat, pressurize after enter reaction tower recycle；
(6), after reaction terminates, bottom reaction tower, discharge coarse biodiesel and the mixture of crude glycerine, subsequently enter
The operations such as follow-up glycerol separation, biodiesel refining.Esterification, ester exchange reaction efficiency are 98.4%.
Embodiment 7:
Specific as follows: (1) methanol adds gentleness through methanol gasifying device and is pressurized to 214 DEG C, and 5.0MPa, from reaction tower
Bottom is injected in reaction tower with diffusion type；(2) glyceride stock is preheated to 80 DEG C from reaction tower top with 30L/min
Flow velocity be sprayed onto in reaction tower, keep temperature 214 DEG C in reaction tower, pressure 5.0MPa；(3) it is perpendicular to
Oils and fats landing direction equidistant parallel arranges 3 blocks of sieve traies, and on column plate, screen-aperture size is 20mm, sieve aperture
Open ratio of plate is 5.0%；(4) monitored the pressure of every layer of sieve tray by Pressure gauge, regulation controls sieve aperture
The thickness that on column plate, oils and fats is piled up is 20mm；(5) excessive methanol enters Methanol Recovery from reaction tower top exit
Tower, then enter back into methanol gasifying device heat, pressurize after enter reaction tower recycle；(6) reaction terminates
After, bottom reaction tower, discharge coarse biodiesel and the mixture of crude glycerine, subsequently enter follow-up glycerol and divide
From operations such as, biodiesel refinings.Esterification, ester exchange reaction efficiency are 97.1.
Embodiment 8:
Specific as follows: (1) methanol adds gentleness through methanol gasifying device and is pressurized to 220 DEG C, and 5.5MPa, from reaction tower
Bottom is injected in reaction tower with diffusion type；(2) glyceride stock be preheated to 120 DEG C from reaction tower top with
The flow velocity of 30L/min is sprayed onto in reaction tower, keeps temperature 220 DEG C in reaction tower, pressure 5.5MPa；(3)
Being perpendicular to oils and fats landing direction equidistant parallel and arrange 9 blocks of sieve traies, on column plate, screen-aperture size is
40mm, sieve tray percent opening is 10%；(4) monitored the pressure of every layer of sieve tray by Pressure gauge, adjust
It is 100mm that joint controls the thickness that on sieve tray, oils and fats is piled up；(5) excessive methanol is from reaction tower top exit
Enter methanol distillation column, then enter back into methanol gasifying device heat, pressurize after enter reaction tower recycle；
(6), after reaction terminates, bottom reaction tower, discharge coarse biodiesel and the mixture of crude glycerine, subsequently enter
The operations such as follow-up glycerol separation, biodiesel refining.Esterification, ester exchange reaction efficiency are 98.3%.
The foregoing is only presently preferred embodiments of the present invention, not in order to limit the present invention, all at this
Within bright spirit and principle, any modification, equivalent substitution and improvement etc. made, should be included in this
Within bright protection domain.
Claims (7)
1. the esterification of a biodiesel, ester exchange reaction method, it is characterised in that comprise the steps:
(1) methanol is after methanol gasifying device is heated, pressurizeed, and gasification temperature is 84 DEG C～220 DEG C, pressure
For 0.2MPa～5.5MPa, making methanol be in nearly subcritical state, methanol gas uses porous type pipeline from instead
Tower bottom is answered to inject in reaction tower with this state；
(2) raw oil material is preheating to 80 DEG C～120 DEG C by heater, then from reaction tower top with necessarily
Flow velocity is sprayed onto in reaction tower, and gaseous methanol the most inversely interts with the oils and fats drop landed during ascension；
(3) keeping and the temperature that controls in reaction tower is 84 DEG C～220 DEG C, pressure is 0.2MPa～5.5MPa,
And methanol is in subcritical state under this temperature and pressure, methanol and oils and fats dissolve each other, two interphase mass transfers
The rapidest abundant；
(4) for extending raw oil material and methanol time of contact and response time, reaction tower is perpendicular to oils and fats
Landing direction equidistant parallel arranges 3～9 blocks of sieve traies, by the sieve tray in described reaction tower to oils and fats
Carry out stop, the deceleration of 3～9 times；
(5) every block of sieve tray is provided with Pressure gauge and liquidometer, observes every layer of sieve tray by Pressure gauge
Between pressure, observe, by liquidometer, the thickness that glyceride stock is piled up on sieve tray；
(6) excessive methanol enters methanol distillation column from reaction tower top exit, then enters back into methanol gasifying device
Heat, pressurize after enter reaction tower recycle；
(7), after reaction terminates, bottom reaction tower, coarse biodiesel and the mixture of crude glycerine are discharged, subsequently
Enter the operations such as follow-up glycerol separation, biodiesel refining.
The esterification of a kind of biodiesel the most according to claim 1, ester exchange reaction method, its feature
Be: described step (1), methanol need to heat through methanol gasifying device, pressurize after to reach one the most subcritical
State could meet the reaction condition of the method.
The esterification of a kind of biodiesel the most according to claim 1, ester exchange reaction method, its feature
It is: described step (5), by the size in aperture, sieve on the charging rate of raw oil material, sieve tray
The control valve of hole column plate percent opening and connection sieve tray both sides adjusts sieve tray and piles up the thickness of oil layer
Degree.
The esterification of a kind of biodiesel the most according to claim 3, ester exchange reaction method, its feature
It is: the charging rate of described raw oil material is 30L/min～100L/min.
The esterification of a kind of biodiesel the most according to claim 3, ester exchange reaction method, its feature
It is: on described sieve tray, the size in aperture is 10mm～50mm.
The esterification of a kind of biodiesel the most according to claim 3, ester exchange reaction method, its feature
It is: described sieve tray percent opening controls 5%～10%.
The esterification of a kind of biodiesel the most according to claim 3, ester exchange reaction method, its feature
It is: the control thickness that on described sieve tray, oils and fats is piled up is generally 10mm～100mm.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108949366A (en) * | 2018-07-13 | 2018-12-07 | 中国科学院青岛生物能源与过程研究所 | A kind of ester exchange process and device can be used for producing biodiesel |
| 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 |
| CN114854498A (en) * | 2022-04-07 | 2022-08-05 | 湖北天基生物能源科技发展有限公司 | Method for esterifying kitchen waste oil and fat with subcritical gaseous methanol |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103224838A (en) * | 2013-05-20 | 2013-07-31 | 阳谷县凯歌新能源生物科技有限公司 | Esterification reaction tower for producing biodiesel |
| CN103242966A (en) * | 2013-05-20 | 2013-08-14 | 阳谷县凯歌新能源生物科技有限公司 | Technology process for producing biodiesel and key preparation device |
| CN203728807U (en) * | 2014-02-28 | 2014-07-23 | 上海中器环保科技有限公司 | Esterification reaction tower for biodiesel |
-
2015
- 2015-08-27 CN CN201510536907.4A patent/CN106190591A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103224838A (en) * | 2013-05-20 | 2013-07-31 | 阳谷县凯歌新能源生物科技有限公司 | Esterification reaction tower for producing biodiesel |
| CN103242966A (en) * | 2013-05-20 | 2013-08-14 | 阳谷县凯歌新能源生物科技有限公司 | Technology process for producing biodiesel and key preparation device |
| CN203728807U (en) * | 2014-02-28 | 2014-07-23 | 上海中器环保科技有限公司 | Esterification reaction tower for biodiesel |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108949366A (en) * | 2018-07-13 | 2018-12-07 | 中国科学院青岛生物能源与过程研究所 | A kind of ester exchange process and device can be used for producing biodiesel |
| 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 |
| CN114854498A (en) * | 2022-04-07 | 2022-08-05 | 湖北天基生物能源科技发展有限公司 | Method for esterifying kitchen waste oil and fat with subcritical gaseous methanol |
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