CN103159595A - Method for preparing phenolic compound by liquefaction of salix mongolica - Google Patents
Method for preparing phenolic compound by liquefaction of salix mongolica Download PDFInfo
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- CN103159595A CN103159595A CN2013100701416A CN201310070141A CN103159595A CN 103159595 A CN103159595 A CN 103159595A CN 2013100701416 A CN2013100701416 A CN 2013100701416A CN 201310070141 A CN201310070141 A CN 201310070141A CN 103159595 A CN103159595 A CN 103159595A
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- 238000000034 method Methods 0.000 title claims abstract description 83
- 241000124033 Salix Species 0.000 title claims abstract description 34
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 title claims abstract description 34
- 150000002989 phenols Chemical class 0.000 title claims abstract description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 68
- 239000003960 organic solvent Substances 0.000 claims abstract description 15
- 239000012075 bio-oil Substances 0.000 claims abstract description 12
- 239000007790 solid phase Substances 0.000 claims abstract description 12
- 239000007788 liquid Substances 0.000 claims abstract description 11
- 238000003756 stirring Methods 0.000 claims abstract description 11
- 239000007791 liquid phase Substances 0.000 claims abstract description 10
- 239000011541 reaction mixture Substances 0.000 claims abstract description 10
- 238000001914 filtration Methods 0.000 claims abstract description 7
- 238000001027 hydrothermal synthesis Methods 0.000 claims abstract description 5
- 150000002894 organic compounds Chemical class 0.000 claims abstract description 5
- 239000012074 organic phase Substances 0.000 claims abstract description 5
- 238000000638 solvent extraction Methods 0.000 claims abstract description 3
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 claims description 72
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 claims description 36
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims description 26
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 9
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 claims description 8
- 239000000126 substance Substances 0.000 claims description 7
- 238000000895 extractive distillation Methods 0.000 claims description 6
- 239000007787 solid Substances 0.000 claims description 6
- 239000008399 tap water Substances 0.000 claims description 6
- 235000020679 tap water Nutrition 0.000 claims description 6
- 238000010792 warming Methods 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 4
- 210000002966 serum Anatomy 0.000 claims description 3
- 239000002253 acid Substances 0.000 claims description 2
- -1 lipid acid Chemical class 0.000 claims description 2
- 238000010298 pulverizing process Methods 0.000 claims description 2
- 239000012071 phase Substances 0.000 abstract description 9
- 238000005516 engineering process Methods 0.000 abstract description 4
- 238000001816 cooling Methods 0.000 abstract 1
- 238000010438 heat treatment Methods 0.000 abstract 1
- 239000011261 inert gas Substances 0.000 abstract 1
- 238000004065 wastewater treatment Methods 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 15
- 239000000295 fuel oil Substances 0.000 description 13
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 9
- CHWNEIVBYREQRF-UHFFFAOYSA-N 4-Ethyl-2-methoxyphenol Chemical compound CCC1=CC=C(O)C(OC)=C1 CHWNEIVBYREQRF-UHFFFAOYSA-N 0.000 description 8
- 238000004821 distillation Methods 0.000 description 8
- 238000011084 recovery Methods 0.000 description 7
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 6
- 230000008901 benefit Effects 0.000 description 4
- LHGVFZTZFXWLCP-UHFFFAOYSA-N guaiacol Chemical compound COC1=CC=CC=C1O LHGVFZTZFXWLCP-UHFFFAOYSA-N 0.000 description 4
- 229960001867 guaiacol Drugs 0.000 description 4
- 239000000843 powder Substances 0.000 description 4
- 239000004576 sand Substances 0.000 description 4
- 239000002002 slurry Substances 0.000 description 4
- 239000002028 Biomass Substances 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 238000004817 gas chromatography Methods 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 150000001298 alcohols Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- FFBHFFJDDLITSX-UHFFFAOYSA-N benzyl N-[2-hydroxy-4-(3-oxomorpholin-4-yl)phenyl]carbamate Chemical compound OC1=C(NC(=O)OCC2=CC=CC=C2)C=CC(=C1)N1CCOCC1=O FFBHFFJDDLITSX-UHFFFAOYSA-N 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000002290 gas chromatography-mass spectrometry Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229920003987 resole Polymers 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
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Abstract
The invention belongs to the salix mongolica resource utilization field, and concretely relates to a method for preparing a phenolic compound by directly reusing process water generated by hydro-thermal liquefaction of salix mongolica. The method comprises the following steps: dumping the crushed salix mongolica in a high pressure reaction vessel to form a mixed liquor with a certain solid-liquid mass ratio, filling inert gas with a certain pressure in a reaction vessel, stirring and heating to the temperature of 150-350 DEG C, keeping for 1-180 minutes, rapidly cooling to room temperature, collecting a reaction mixture, filtering the reaction mixture and separating to obtain a solid phase and a liquid phase, wherein the liquid phase is the process water which is directly reused as a liquefaction medium for next hydro-thermal liquefaction, and the organic compound in the organic solvent extraction process water can be used in advance, and the surplus water phase is taken as a liquefaction medium for next hydro-thermal reaction. The solid phase and the process water are extracted by an organic solvent, the organic phase is separated and filtered to remove the organic solvent to obtain bio oil. The bio oil contains abundant phenolic compound. The hydro-thermal liquefaction process water can be directly reused for simplifying the technology flow, the waste water treatment is reduced, and generation of the phenolic compound can be simultaneously promoted.
Description
Technical field
The invention belongs to salix monogolica application technology as the second resource field, being specifically related to a kind of (is mainly phenol with salix monogolica hydro-thermal liquefaction process water direct reuse liquefaction preparation phenolic compound, methyl catechol, 4-ethyl-2-methoxyphenol and 2,6-syringol) method.
Background technology
Salix monogolica is that a class energy for growth is strong, adapts to the plant of drought environment.These characteristics make them become the first-selection of checking winds and fixing drifting sand, and have planted large stretch of area in the NW China arid area.These plants need stump at set intervals, so every annual meeting produces a large amount of desert shrub branches, have the wide prospect of utilizing.
Hydro-thermal liquefaction processing biomass are a kind of novel treatment process, have that raw material sources are wide, reaction conditions and equipment simply and simple operation and other advantages.In recent years, utilize the biomass liquefying production of chemicals to begin to cause people's attention, the license notification number is that the patent of invention of CN101245566 B is the method that phenol selective liquefaction Mierocrystalline cellulose is produced bio-based resol.Number of patent application is that the patent of invention of 201010291801.X is a kind of method with the desert shrub preparing liquid fuel by hydrothermal liquification, and this method utilizes the hydro-thermal liquifying method that salix monogolica is converted into liquid fuel.Yet, can produce a large amount of process waters after the hydro-thermal liquefaction reaction, this is a kind of waste water that contains gas chromatography, and chemical oxygen demand (COD) is high, and intractability is large, has greatly limited the large-scale promotion of hydro-thermal liquefaction.If so with the process water direct reuse that produces after hydro-thermal liquefaction as the liquefaction medium of hydro-thermal liquefaction reaction next time, so both simplified the flow process of hydro-thermal liquefaction, also reduced the cost of process water processing.Simultaneously, small organic molecule such as the acetic acid in hydro-thermal liquefaction process water, phenol, alcohols etc. can promote the hydro-thermal liquefaction reaction, strengthen the generation of phenolic compound.
Summary of the invention
The object of the present invention is to provide a kind of method that the liquefaction of salix monogolica hydro-thermal liquefaction process water direct reuse is prepared phenolic compound, being specially the phenolic compound that utilizes hydro-thermal liquefaction that the salix monogolica branch is changed into to have high marketable value (is mainly phenol, methyl catechol, 4-ethyl-2-methoxyphenol and 2,6-syringol etc.), the process water direct reuse that produces by hydro-thermal is liquefied is as the liquefaction medium after hydro-thermal liquefies next time, the flow process of simplification hydro-thermal liquefaction and minimizing process water processing cost form one and overlap complete hydro-thermal liquefaction reaction system.
Thinking of the present invention is that salix monogolica produces a large amount of branch resources every year as a kind of main plant of checking winds and fixing drifting sand, and still but can not get effectively utilizing.Hydro-thermal liquefied wood quality of biomass can obtain phenolic compound, both is joined together, with the maximization of economic benefit of salix monogolica.In addition, the process water direct reuse that produces after the hydro-thermal liquefaction reaction is simplified flow process and the minimizing process water processing cost of hydro-thermal liquefaction.
Technological line of the present invention as shown in Figure 1, its key step is as follows:
(1) collect the salix monogolica branch, after pulverizing, pour in autoclave, add water and mix and make that to form the solid-liquid mass ratio be the mixed solution of 1:60 ~ 1:2;
(2) be filled with the N of 0 ~ 6MPa in the autoclave
2, stir and be warming up to 150 ~ 350 ℃ and keep 1 ~ 180min, be cooled to rapidly room temperature, collect reaction mixture;
(3) be liquid phase and solid phase with the reaction mixture filtering separation, liquid phase is process water, and the process water direct reuse is as the liquefaction medium of hydro-thermal liquefaction next time; Also can first use organic solvent extraction process water organic compound wherein, be rich in lipid acid and phenolic compound in this organic compound, the residue water is used as the liquefaction medium of hydro-thermal reaction next time as backwater.
(4) with organic solvent, solid phase is carried out extractive distillation, obtain organic phase and solid residue, the organic solvent 2 of removing in organic phase namely obtains bio oil, be rich in phenolic compound (mainly comprising phenol, methyl catechol, 4-ethyl-2-methoxyphenol, 2,6-syringol etc.) in bio oil.Organic solvent can reclaim, recycle.
(5) reuse process water in step (3) or backwater and directly pulverize branch configuration mixed serum with salix monogolica and continue above-mentioned hydro-thermal reaction step, separation obtaining bio oil.
Described organic solvent for the extractive distillation process water is ethyl acetate, methylene dichloride or ether etc.
Described organic solvent for the extractive distillation solid phase is tetrahydrofuran (THF), ethyl acetate, methylene dichloride or ether etc.
Hydro-thermal liquefaction process water or backwater can unlimitedly be reused as the liquefaction medium of salix monogolica, according to the requirement of reaction solid-liquid mass ratio, suitably add tap water.
Result of the present invention utilizes gas-chromatography and GC-MS that the composition of bio oil is analyzed, and shows that the direct reuse of process water is feasible after hydro-thermal liquefaction, and greatly promotes the content of phenolic compound in the increase of bio oil productive rate and bio oil.
Take full advantage of for the salix monogolica branch, formed the double effects of checking winds and fixing drifting sand with economic benefit, improved greatly economic worth and the ecological value of salix monogolica.The hydro-thermal liquefaction technology is simple to operate, and cost is low, is easy to large-scale promotion.And the process water direct reuse with the hydro-thermal liquefaction reaction produces can make the hydro-thermal LNG Lquified Process Flow more simplify, and cost is lower; For the sand ground arid area, the process water direct reuse can effectively solve shortage of water problem and waste water handling problem simultaneously.
Description of drawings
Fig. 1 is experimental procedure figure.
Fig. 2 is embodiment 1, example 2, example 3 and the heavy oil of example 4 generations and the oil yield rate change curve of middle oil.
Embodiment
The invention is further illustrated by the following examples, but be not limitation of the invention.
Embodiment 1
Salix monogolica is pulverized, get 30g salix monogolica powder and pour in the 250ml autoclave and add 150ml distilled water, stir the furnishing slurries, be filled with 2MPa N to reactor
2, warming while stirring to 300 ℃ keeps 10min, and logical tap water makes and is cooled to room temperature, pours out reaction mixture, and cleans the still chamber with tetrahydrofuran (THF); The mixture filtration is divided into solid, liquid two-phase, and liquid phase is process water.With the 150ml tetrahydrofuran (THF), solid phase is carried out extracting, the separating and extracting extract filters the tetrahydrofuran (THF) phase with Büchner funnel, then underpressure distillation recovery tetrahydrofuran (THF) namely obtains heavy oil; With ether, process water is extracted, ether reclaims ether through underpressure distillation and namely obtains middle oil, and water is backwater, gives over to experiment next time and uses.Be rich in phenolic compound in heavy oil and middle oil.
Embodiment 2
Salix monogolica is pulverized, get 30g salix monogolica powder and pour in the 250ml autoclave, add the process water of embodiment 1 acquisition as medium, stir the furnishing slurries, be filled with 2MPa N to reactor
2, warming while stirring to 300 ℃ keeps 10min, and logical tap water makes and is cooled to room temperature, pours out reaction mixture, and cleans the still chamber with tetrahydrofuran (THF); The mixture filtration is divided into solid, liquid two-phase, and liquid phase is process water.With the 150ml tetrahydrofuran (THF), solid phase is carried out extracting, the separating and extracting extract filters the tetrahydrofuran (THF) phase with Büchner funnel, then underpressure distillation recovery tetrahydrofuran (THF) namely obtains heavy oil.Directly add another reactor as the liquefaction medium of hydro-thermal liquefaction reaction next time process water, then repeat top process 1 time, obtain heavy oil and process water after process water reuse 1 secondary response.With ether, process water is extracted at last, then underpressure distillation recovery ether namely obtains middle oil.
Embodiment 3
Salix monogolica is pulverized, gets 30g salix monogolica powder and pour process water that the 250ml high pressure adds embodiment 12 into as medium,, stir the furnishing slurries, be filled with 2MPa N to reactor
2, warming while stirring to 300 ℃ keeps 10min, and logical tap water makes and is cooled to room temperature, pours out reaction mixture, and cleans the still chamber with tetrahydrofuran (THF); The mixture filtration is divided into solid, liquid two-phase, and liquid phase is process water.With the 150ml tetrahydrofuran (THF), solid phase is carried out extracting, the separating and extracting extract filters the tetrahydrofuran (THF) phase with Büchner funnel, then underpressure distillation recovery tetrahydrofuran (THF) namely obtains heavy oil.Directly add another reactor as the liquefaction medium of hydro-thermal liquefaction reaction next time process water, the process above repeating 2 times obtains heavy oil and process water after process water reuse 2 secondary responses.With ether, process water is extracted at last, then underpressure distillation recovery ether namely obtains middle oil.
Embodiment 4
Salix monogolica is pulverized, get 30g salix monogolica powder and pour process water that the 250ml high pressure adds embodiment 12 into as medium, stir the furnishing slurries, be filled with 2MPa N to reactor
2, warming while stirring to 300 ℃ keeps 10min, and logical tap water makes and is cooled to room temperature, pours out reaction mixture, and cleans the still chamber with tetrahydrofuran (THF); The mixture filtration is divided into solid, liquid two-phase, and liquid phase is process water.With the 150ml tetrahydrofuran (THF), solid phase is carried out extracting, the separating and extracting extract filters the tetrahydrofuran (THF) phase with Büchner funnel, then underpressure distillation recovery tetrahydrofuran (THF) namely obtains heavy oil.Directly add another reactor as the liquefaction medium of hydro-thermal liquefaction reaction next time process water, the process above repeating 3 times obtains heavy oil and process water after process water reuse 2 secondary responses.With ether, process water is extracted at last, then underpressure distillation recovery ether namely obtains middle oil.
Can find out from accompanying drawing 2, the direct reuse number of times of process water is more, and the oil yield rate of heavy oil and middle oil is just higher, and oil yield rate improves obviously, and total oil yield rate is up to 46%.Declarative procedure water direct reuse not only can be simplified production technique and processing cost, and promotes the hydro-thermal liquefaction reaction of salix monogolica.
Can find out from subordinate list 1, after the direct reuse of process water in heavy oil the kind of phenolic compound change very smallly, essential substance is phenol, methyl catechol, 4-ethyl-2-methoxyphenol and 2,6-syringol; And total content has the trend of rising, so the direct reuse of process water does not change the quality of heavy oil, has strengthened on the contrary the content of phenolic compound.
Can find out from subordinate list 2, the primary product of middle oil is acetic acid and phenolic compound, and in after the direct reuse of process water, the content of the acetic acid in oil and phenolic compound has the trend of rising.So the direct reuse of process water has strengthened the quality of middle oil.
In sum, after hydro-thermal liquefaction, the direct reuse of process water is feasible, and greatly promotes the content of phenolic compound in the increase of bio oil productive rate and bio oil.
Composition and the content of the heavy oil that table 1. embodiment 1, example 2, example 3 and example 4 produce
Annotate:RT.
aBe retention time, unit: minute.
Composition and the content of the middle oil that table 2. embodiment 1, example 2, example 3 and example 4 produce
Annotate:RT.
aBe retention time, unit: minute.
Claims (4)
1. method that salix monogolica hydro-thermal liquefaction process water direct reuse liquefaction is prepared the phenols chemical is characterized in that key step is as follows:
(1) collect the salix monogolica branch, after pulverizing, pour in autoclave, add water and mix and make that to form the solid-liquid mass ratio be the mixed serum of 1:60 ~ 1:2;
(2) be filled with the N of 0 ~ 6MPa in the autoclave
2, stir and be warming up to 150 ~ 350 ℃ and keep 1 ~ 180min, be cooled to rapidly room temperature, collect reaction mixture;
(3) be liquid phase and solid phase with the reaction mixture filtering separation, liquid phase is process water, and the process water direct reuse is as the liquefaction medium of hydro-thermal liquefaction next time; Also can first use organic solvent extraction process water organic compound wherein, be rich in lipid acid and phenolic compound in this organic compound, the residue water is used as the liquefaction medium of hydro-thermal reaction next time as backwater;
(4) with organic solvent, solid phase is carried out extractive distillation, obtain organic phase and solid residue, remove the bio oil that organic solvent in organic phase namely obtains being rich in phenolic compound, organic solvent reclaims, recycles;
(5) reuse process water in step (3) or backwater and directly pulverize branch configuration mixed serum with salix monogolica and continue above-mentioned hydro-thermal reaction step, separation obtaining bio oil.
2. the method that the liquefaction of salix monogolica hydro-thermal liquefaction process water direct reuse is prepared the phenols chemical as claimed in claim 1, is characterized in that, the organic solvent that is used for the extractive distillation process water in described step (3) is ethyl acetate, methylene dichloride or ether.
3. as claimed in claim 1 salix monogolica hydro-thermal liquefaction process water direct reuse is liquefied prepares the method for phenols chemical, it is characterized in that, the organic solvent that is used for the extractive distillation solid phase in described step (4) is tetrahydrofuran (THF), ethyl acetate, methylene dichloride or ether.
4. as claimed in claim 1 salix monogolica hydro-thermal liquefaction process water direct reuse is liquefied prepares the method for phenols chemical, it is characterized in that hydro-thermal liquefaction process water or backwater can unlimitedly be reused as the liquefaction medium of salix monogolica, according to the requirement of reaction solid-liquid mass ratio, suitably add tap water.
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| CN201310070141.6A CN103159595B (en) | 2013-03-06 | 2013-03-06 | A kind of method that salix monogolica liquefaction prepares phenolic compound |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105037111A (en) * | 2015-05-28 | 2015-11-11 | 复旦大学 | Method for separating and purifying 2,6-dimethoxy phenol and acetosyringone from biological oil |
| CN108441248A (en) * | 2018-04-03 | 2018-08-24 | 北京林业大学 | A method of being prepared as raw material using discarded Poplar Powder has antioxidative bio oil |
| CN110373221A (en) * | 2019-08-20 | 2019-10-25 | 沈阳航空航天大学 | A kind of extraction separating method reducing biomass by hydro-thermal liquefaction oil moisture |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101955787A (en) * | 2010-09-26 | 2011-01-26 | 复旦大学 | Method for preparing liquid fuel by performing hydrothermal liquefaction on sandy shrubs |
| CN102899069A (en) * | 2012-10-30 | 2013-01-30 | 复旦大学 | Separating and upgrading method of bio-oil by column chromatography |
-
2013
- 2013-03-06 CN CN201310070141.6A patent/CN103159595B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101955787A (en) * | 2010-09-26 | 2011-01-26 | 复旦大学 | Method for preparing liquid fuel by performing hydrothermal liquefaction on sandy shrubs |
| CN102899069A (en) * | 2012-10-30 | 2013-01-30 | 复旦大学 | Separating and upgrading method of bio-oil by column chromatography |
Non-Patent Citations (2)
| Title |
|---|
| SUDONG YIN ET AL.,: "Hydrothermal liquefaction of cellulose to bio-oil under acidic, neutral and alkaline conditions", 《APPLIED ENERGY》 * |
| 白爱玲等: "木质素制备燃料及化学品研究进展", 《现代化工》 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105037111A (en) * | 2015-05-28 | 2015-11-11 | 复旦大学 | Method for separating and purifying 2,6-dimethoxy phenol and acetosyringone from biological oil |
| CN105037111B (en) * | 2015-05-28 | 2017-03-01 | 复旦大学 | A kind of method of separating-purifying 2,6 syringol and acetosyringone from bio oil |
| CN108441248A (en) * | 2018-04-03 | 2018-08-24 | 北京林业大学 | A method of being prepared as raw material using discarded Poplar Powder has antioxidative bio oil |
| CN110373221A (en) * | 2019-08-20 | 2019-10-25 | 沈阳航空航天大学 | A kind of extraction separating method reducing biomass by hydro-thermal liquefaction oil moisture |
| CN110373221B (en) * | 2019-08-20 | 2021-06-29 | 沈阳航空航天大学 | Extraction separation method for reducing water content of biomass hydrothermal liquefied oil |
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Owner name: INNER MONGOLIA JINLVYUAN GREEN ENGINEERING LIMITED Effective date: 20130809 |
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Inventor after: Zhang Shicheng Inventor after: Bao Hongguang Inventor after: Li Changjun Inventor after: Chen Zhongwu Inventor after: Chen Jianmin Inventor before: Zhang Shicheng Inventor before: Li Changjun Inventor before: Chen Zhongwu Inventor before: Bao Hongguang Inventor before: Chen Jianmin |
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Free format text: CORRECT: INVENTOR; FROM: ZHANG SHICHENG LI CHANGJUN CHEN ZHONGWU BAO HONGGUANG CHEN JIANMIN TO: ZHANG SHICHENG BAO HONGGUANG LI CHANGJUN CHEN ZHONGWU CHEN JIANMIN |
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Effective date of registration: 20130809 Address after: 200433 Handan Road, Shanghai, No. 220, No. Applicant after: Fudan University Applicant after: Inner Mongolia Jinlvyuan Green Engineering Limited Liability Company Address before: 200433 Handan Road, Shanghai, No. 220, No. Applicant before: Fudan University |
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