CN103215140A - Method for continuously producing biodiesel without catalysts - Google Patents
Method for continuously producing biodiesel without catalysts Download PDFInfo
- Publication number
- CN103215140A CN103215140A CN2013101715187A CN201310171518A CN103215140A CN 103215140 A CN103215140 A CN 103215140A CN 2013101715187 A CN2013101715187 A CN 2013101715187A CN 201310171518 A CN201310171518 A CN 201310171518A CN 103215140 A CN103215140 A CN 103215140A
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- Prior art keywords
- tower
- continuously
- reaction
- biofuel
- methyl esters
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- 238000000034 method Methods 0.000 title claims abstract description 17
- 239000003225 biodiesel Substances 0.000 title claims abstract description 14
- 239000003054 catalyst Substances 0.000 title abstract 2
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 81
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims abstract description 48
- 238000006243 chemical reaction Methods 0.000 claims abstract description 29
- 150000004702 methyl esters Chemical class 0.000 claims abstract description 29
- 238000004821 distillation Methods 0.000 claims abstract description 12
- 230000032050 esterification Effects 0.000 claims abstract description 8
- 238000005886 esterification reaction Methods 0.000 claims abstract description 8
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 7
- 238000004332 deodorization Methods 0.000 claims abstract description 6
- 235000014113 dietary fatty acids Nutrition 0.000 claims abstract description 4
- 229930195729 fatty acid Natural products 0.000 claims abstract description 4
- 239000000194 fatty acid Substances 0.000 claims abstract description 4
- 150000004665 fatty acids Chemical class 0.000 claims abstract description 4
- 125000005456 glyceride group Chemical group 0.000 claims abstract description 4
- 230000007062 hydrolysis Effects 0.000 claims abstract description 4
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 4
- 239000002551 biofuel Substances 0.000 claims description 31
- 235000011187 glycerol Nutrition 0.000 claims description 20
- 239000000470 constituent Substances 0.000 claims description 6
- 239000012535 impurity Substances 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 235000019387 fatty acid methyl ester Nutrition 0.000 claims description 4
- 239000002994 raw material Substances 0.000 claims description 4
- 238000005809 transesterification reaction Methods 0.000 claims description 4
- 241000282326 Felis catus Species 0.000 claims description 3
- 230000018044 dehydration Effects 0.000 claims description 3
- 238000006297 dehydration reaction Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 239000000047 product Substances 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 9
- 241001465754 Metazoa Species 0.000 abstract description 4
- 230000000813 microbial effect Effects 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 4
- 239000002351 wastewater Substances 0.000 abstract description 4
- 239000004519 grease Substances 0.000 abstract 2
- 125000004185 ester group Chemical group 0.000 abstract 1
- 238000010438 heat treatment Methods 0.000 abstract 1
- 238000011031 large-scale manufacturing process Methods 0.000 abstract 1
- 150000002632 lipids Chemical class 0.000 abstract 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 abstract 1
- 238000005086 pumping Methods 0.000 abstract 1
- 230000036632 reaction speed Effects 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 10
- 235000019198 oils Nutrition 0.000 description 10
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 239000010775 animal oil Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 235000015112 vegetable and seed oil Nutrition 0.000 description 3
- 239000008158 vegetable oil Substances 0.000 description 3
- 239000010426 asphalt Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000010025 steaming Methods 0.000 description 2
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000006353 environmental stress Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- 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
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Fats And Perfumes (AREA)
- Liquid Carbonaceous Fuels (AREA)
Abstract
The invention discloses a method for continuously producing biodiesel without catalysts. The method comprises the following steps of: heating and pressurizing waste animal and plant grease, microbial grease and the like; performing lipid hydrolysis with methanol, fatty acid esterification and ester exchange reaction with glyceride in a biodiesel reaction tower; and pumping the reaction products to a glycerol distillation tower, a methyl ester deodorization tower and a methyl distillation tower continuously to obtain the biodiesel. The method is continuous, quick in reaction speed, low in production cost, simple to operate, free from process wastewater, stable and reliable in quality and suitable for large-scale production.
Description
Technical field
The present invention relates to the production of biodiesel technical field, specifically is a kind of method of catalyst-free continuously producing biodiesel.
Background technology
Biofuel also claims fatty acid methyl ester, it be waste animal and vegetable oil, microbial oil etc. as raw material, obtain through esterification, transesterification reaction with methyl alcohol low-carbon alcohol such as (or ethanol).Biofuel becomes a kind of fine petroleum diesel substitute with its unique recyclability and green environmental protection, is considered to solve global energy crisis, one of the environmental stress of releiving, control topsoil optimal approach.
At present, the processing method of China's suitability for industrialized production biofuel mainly contains two kinds, (1) chemical method: adopt this method production biofuel comparatively ripe, because of using acid, alkali as catalyzer, be easy to generate a large amount of waste water.(2) biological enzyme: adopting this comparatively environmental protection of method production biofuel, is not shortcoming such as very stable but exist long, technology of production cost height, reaction times.
Summary of the invention
The invention provides a kind of method of catalyst-free continuously producing biodiesel, solve existing production method and easily produce a large amount of waste water, production cost height and technology problem of unstable.
The method of this catalyst-free continuously producing biodiesel of the present invention is as follows:
A, stock oil (waste animal and vegetable oil, microbial oil etc.) are through removal of impurities, vacuum flashing dehydration, and moisture content requires in 0.1%;
B, removal of impurities, dehydrated raw material oil pumped up to 1.3MPa～4.0MPa carry, be heated to 180 ℃～220 ℃, enter from biofuel reaction tower top continuously through preheater;
C, the auxiliary material methyl alcohol of purity＞98% pumped up to 1.3MPa～4.0MPa carry, be heated to 180 ℃～220 ℃, enter from biofuel reaction tower bottom continuously through preheater;
D, stock oil is from top to bottom in the biofuel reaction tower, methanol gas is driven in the wrong direction from bottom to top and is contacted, and fat hydrolysis, fatty acid esterification and glyceride transesterification reaction take place, and generates fatty acid methyl ester and glycerine, be reflected at 1.3MPa～4.0MPa, carry out under 180 ℃～220 ℃ conditions;
E, excessive methanol gas entrainment the water of reaction generation and are discharged from biofuel reaction cat head, reclaim methyl alcohol continuously through methanol distillation column, the methyl alcohol of purity＞98% can recycle for the biofuel reaction tower, and separates the water of discharging the esterification generation from the Methanol Recovery tower bottom;
F, emit reaction product from biofuel reaction tower bottom: the mixture of thick methyl esters and raw glycerine;
G, the mixture of thick methyl esters of reaction product and raw glycerine is squeezed in the glycerol distillation tower continuously, temperature is controlled at 160 ℃～185 ℃, pressure-controlling-0.08MPa～-0.1MPa, remove raw glycerine and other light constituent materials continuously;
H, the thick methyl esters that will remove behind the raw glycerine are squeezed in methyl esters deodorization tower and the methyl ester distilled tower continuously, temperature is controlled at 175 ℃～200 ℃, pressure-controlling-0.08MPa～-0.1MPa, light constituent in the thick methyl esters (stink thing) is all removed away, enter methyl ester distilled tower then continuously, under same pressure, the recovered temperature scope obtains smart methyl esters (being biofuel) at 180 ℃～240 ℃ overhead product, and the steaming excess is plant asphalt (a black pin).
Described biofuel reaction tower is three tower cascade connected, stock oil all the time from top to bottom, methanol gas is all the time from bottom to top.
Described biofuel reaction tower, methanol distillation column, glycerol distillation tower, methyl esters deodorization tower, methyl ester distilled tower all are the serialization operation.
Described biofuel reaction tower also can replace with tubular reactor.
The method of this catalyst-free continuously producing biodiesel provided by the invention can realize that serialization, speed of response are fast, low production cost, simple to operate and do not have processing wastewater, steady quality and reliably be fit to scale operation.
Embodiment
Stock oil (waste animal and vegetable oil, microbial oil etc.) is through removal of impurities, vacuum flashing dehydration, and moisture content requires in 0.1%; Removal of impurities, dehydrated raw material oil are pumped up to 1.3MPa～4.0MPa conveying, be heated to 180 ℃～220 ℃, enter from biofuel reaction tower top continuously through preheater; The auxiliary material methyl alcohol of purity＞98% is pumped up to 1.3MPa～4.0MPa conveying, be heated to 180 ℃～220 ℃, enter from biofuel reaction tower bottom continuously through preheater; Stock oil from top to bottom in the biofuel reaction tower, methanol gas is driven in the wrong direction from bottom to top and is contacted, and fat hydrolysis, fatty acid esterification and glyceride transesterification reaction take place, and generates fatty acid methyl ester and glycerine, be reflected at 1.3MPa～4.0MPa, carry out under 180 ℃～220 ℃ conditions; The excessive methanol gas entrainment the water of reaction generation and is discharged from biofuel reaction cat head, reclaim methyl alcohol continuously through methanol distillation column, the methyl alcohol of purity＞98% can recycle for the biofuel reaction tower, and separates the water of discharging the esterification generation from the Methanol Recovery tower bottom; Emit reaction product from biofuel reaction tower bottom: the mixture of thick methyl esters and raw glycerine; The mixture of thick methyl esters of reaction product and raw glycerine is squeezed in the glycerol distillation tower continuously, and temperature is controlled at 160 ℃～185 ℃, pressure-controlling-0.08MPa～-0.1MPa, remove raw glycerine and other light constituent materials continuously; The thick methyl esters that removes behind the raw glycerine is squeezed in methyl esters deodorization tower and the methyl ester distilled tower continuously, temperature is controlled at 175 ℃～200 ℃, pressure-controlling-0.08MPa～-0.1MPa, light constituent in the thick methyl esters (stink thing) is all removed away, enter methyl ester distilled tower then continuously, under same pressure, the recovered temperature scope obtains smart methyl esters (biofuel) at 180 ℃～240 ℃ overhead product, and the steaming excess is plant asphalt (a black pin).
Claims (4)
1. the method for a catalyst-free continuously producing biodiesel is characterized in that as follows:
A, stock oil are through removal of impurities, vacuum flashing dehydration, and moisture content requires in 0.1%;
B, removal of impurities, dehydrated raw material oil pumped up to 1.3MPa～4.0MPa carry, be heated to 180 ℃～220 ℃, enter from biofuel reaction tower top continuously through preheater;
C, the auxiliary material methyl alcohol of purity＞98% pumped up to 1.3MPa～4.0MPa carry, be heated to 180 ℃～220 ℃, enter from biofuel reaction tower bottom continuously through preheater;
D, stock oil is from top to bottom in the biofuel reaction tower, methanol gas is driven in the wrong direction from bottom to top and is contacted, and fat hydrolysis, fatty acid esterification and glyceride transesterification reaction take place, and generates fatty acid methyl ester and glycerine, be reflected at 1.3MPa～4.0MPa, carry out under 180 ℃～220 ℃ conditions;
E, excessive methanol gas entrainment the water of reaction generation and are discharged from biofuel reaction cat head, reclaim methyl alcohol continuously through methanol distillation column, the methyl alcohol of purity＞98% can recycle for the biofuel reaction tower, and separates the water of discharging the esterification generation from the Methanol Recovery tower bottom;
F, emit reaction product from biofuel reaction tower bottom: the mixture of thick methyl esters and raw glycerine;
G, the mixture of thick methyl esters of reaction product and raw glycerine is squeezed in the glycerol distillation tower continuously, temperature is controlled at 160 ℃～185 ℃, pressure-controlling-0.08MPa～-0.1MPa, remove raw glycerine and other light constituent materials continuously;
H, the thick methyl esters that will remove behind the raw glycerine are squeezed in methyl esters deodorization tower and the methyl ester distilled tower continuously, temperature is controlled at 175 ℃～200 ℃, pressure-controlling-0.08MPa～-0.1MPa, light constituent in the thick methyl esters is all removed away, enter methyl ester distilled tower then continuously, under same pressure, the recovered temperature scope obtains smart methyl esters at 180 ℃～240 ℃ overhead product.
2. the method for a kind of catalyst-free continuously producing biodiesel according to claim 1 is characterized in that: described biofuel reaction tower is three tower cascade connected, stock oil all the time from top to bottom, methanol gas is all the time from bottom to top.
3. the method for a kind of catalyst-free continuously producing biodiesel according to claim 1 is characterized in that: described biofuel reaction tower, methanol distillation column, glycerol distillation tower, methyl esters deodorization tower, methyl ester distilled tower all are the serialization operation.
4. the method for a kind of catalyst-free continuously producing biodiesel according to claim 1 is characterized in that: described biofuel reaction tower can replace with tubular reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013101715187A CN103215140A (en) | 2013-03-19 | 2013-03-19 | Method for continuously producing biodiesel without catalysts |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013101715187A CN103215140A (en) | 2013-03-19 | 2013-03-19 | Method for continuously producing biodiesel without catalysts |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103215140A true CN103215140A (en) | 2013-07-24 |
Family
ID=48813309
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013101715187A Pending CN103215140A (en) | 2013-03-19 | 2013-03-19 | Method for continuously producing biodiesel without catalysts |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103215140A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103361185A (en) * | 2013-08-09 | 2013-10-23 | 陈春林 | Non-catalytic production method of biodiesel |
| CN103756790A (en) * | 2014-01-23 | 2014-04-30 | 湖南未名创林生物能源有限公司 | Production method of biodiesel |
| CN105861164A (en) * | 2016-05-03 | 2016-08-17 | 陕西德融新能源股份有限公司 | Technology for producing biodiesel from non-refined fat with no catalyst |
| 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 |
| CN111088115A (en) * | 2019-10-25 | 2020-05-01 | 赵汇川 | Method for synthesizing biodiesel by continuous medium-pressure esterification |
-
2013
- 2013-03-19 CN CN2013101715187A patent/CN103215140A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103361185A (en) * | 2013-08-09 | 2013-10-23 | 陈春林 | Non-catalytic production method of biodiesel |
| CN103756790A (en) * | 2014-01-23 | 2014-04-30 | 湖南未名创林生物能源有限公司 | Production method of biodiesel |
| CN105861164A (en) * | 2016-05-03 | 2016-08-17 | 陕西德融新能源股份有限公司 | Technology for producing biodiesel from non-refined fat with no catalyst |
| 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 |
| CN111088115A (en) * | 2019-10-25 | 2020-05-01 | 赵汇川 | Method for synthesizing biodiesel by continuous medium-pressure esterification |
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Legal Events
| Date | Code | Title | Description |
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| C06 | Publication | ||
| PB01 | Publication | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20130724 |