CN101412745A - Improved process for extracting sterol from vegetable oil asphalt - Google Patents
Improved process for extracting sterol from vegetable oil asphalt Download PDFInfo
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- CN101412745A CN101412745A CNA2008102362478A CN200810236247A CN101412745A CN 101412745 A CN101412745 A CN 101412745A CN A2008102362478 A CNA2008102362478 A CN A2008102362478A CN 200810236247 A CN200810236247 A CN 200810236247A CN 101412745 A CN101412745 A CN 101412745A
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- sterol
- plant oil
- oil asphalt
- temperature
- methods
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- 239000010426 asphalt Substances 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims abstract description 28
- 229930182558 Sterol Natural products 0.000 title claims description 66
- 235000003702 sterols Nutrition 0.000 title claims description 66
- 150000003432 sterols Chemical class 0.000 title claims description 63
- 235000015112 vegetable and seed oil Nutrition 0.000 title abstract 3
- 239000008158 vegetable oil Substances 0.000 title abstract 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 30
- 239000002904 solvent Substances 0.000 claims abstract description 29
- 238000007127 saponification reaction Methods 0.000 claims abstract description 20
- 239000000047 product Substances 0.000 claims abstract description 16
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 15
- 238000003756 stirring Methods 0.000 claims abstract description 12
- 239000000706 filtrate Substances 0.000 claims abstract description 9
- 239000003513 alkali Substances 0.000 claims abstract description 8
- 239000003960 organic solvent Substances 0.000 claims abstract description 6
- 238000006243 chemical reaction Methods 0.000 claims description 32
- 239000010773 plant oil Substances 0.000 claims description 28
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims description 22
- 238000010992 reflux Methods 0.000 claims description 19
- 239000000284 extract Substances 0.000 claims description 15
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 claims description 14
- 238000001816 cooling Methods 0.000 claims description 13
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 claims description 12
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 12
- 239000012043 crude product Substances 0.000 claims description 8
- 238000001291 vacuum drying Methods 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 7
- 238000010828 elution Methods 0.000 claims description 6
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical group C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 3
- 239000012295 chemical reaction liquid Substances 0.000 claims description 2
- 239000002994 raw material Substances 0.000 abstract description 4
- 230000008020 evaporation Effects 0.000 abstract 1
- 238000001704 evaporation Methods 0.000 abstract 1
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 18
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 18
- 238000005406 washing Methods 0.000 description 7
- 239000002253 acid Substances 0.000 description 6
- 239000000376 reactant Substances 0.000 description 6
- 150000002632 lipids Chemical class 0.000 description 5
- 235000002378 plant sterols Nutrition 0.000 description 5
- 239000003921 oil Substances 0.000 description 4
- 235000019198 oils Nutrition 0.000 description 4
- -1 sterol ester Chemical class 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 2
- 235000014113 dietary fatty acids Nutrition 0.000 description 2
- 239000000194 fatty acid Substances 0.000 description 2
- 229930195729 fatty acid Natural products 0.000 description 2
- 125000005908 glyceryl ester group Chemical group 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000012805 post-processing Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 244000068988 Glycine max Species 0.000 description 1
- 235000010469 Glycine max Nutrition 0.000 description 1
- 235000019483 Peanut oil Nutrition 0.000 description 1
- 235000019484 Rapeseed oil Nutrition 0.000 description 1
- 238000006136 alcoholysis reaction Methods 0.000 description 1
- 238000009874 alkali refining Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000001851 biosynthetic effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 235000012343 cottonseed oil Nutrition 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000004332 deodorization Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000032050 esterification Effects 0.000 description 1
- 238000005886 esterification reaction Methods 0.000 description 1
- 150000004665 fatty acids Chemical class 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 235000021588 free fatty acids Nutrition 0.000 description 1
- 229940088597 hormone Drugs 0.000 description 1
- 239000005556 hormone Substances 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 235000012054 meals Nutrition 0.000 description 1
- 229930014626 natural product Natural products 0.000 description 1
- LYGJENNIWJXYER-UHFFFAOYSA-N nitromethane Chemical compound C[N+]([O-])=O LYGJENNIWJXYER-UHFFFAOYSA-N 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 239000000312 peanut oil Substances 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 239000000344 soap Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 235000013311 vegetables Nutrition 0.000 description 1
Abstract
The invention discloses an improved method for extracting phytosterol from asphalt of vegetable oil. The method has a simple process, high product purity and low product cost. The improved method comprises the following steps: (1) the asphalt of the vegetable oil is heated and melted at a temperature of between 80 and 100 DEG C, is added with alkali and water, is kept at the temperature, is continuously stirred and saponified for 0.5 hour, is added with hot water, is continuously heated, reflows and reacts for 1.5 to 2.5 hours; a saponification reaction solution is cooled and delaminated; the collected unsaponified layer is added with alcohol with 2 to 3 times of the weight of the raw material of the asphalt, is added with alkali, is heated to a temperature of between 75 and 85 DEG C, reflows for 3 to 5 hours and is stopped to heat and stir; after the solution is cooled to the temperature of 50 DEG C, the solution is added with hot water and continuously reacts and reflows for 10 to 30 minutes; and after the solution is fully cooled, the phytosterol is precipitated out and filtered to obtain a coarse product of the phytosterol; and (2) the coarse phytosterol is eluted through an organic solvent; a filtrate evaporation solvent is put to a vacuum dry box and is dried at a temperature of between 50 and 60 DEG C to obtain the phytosterol product.
Description
Technical field
The present invention relates to a kind of method of extracting sterol, from plant oil asphalt, extract improving one's methods of sterol more specifically to a kind of.
Background technology
Plant sterol is the natural compounds of a class biologically active, extensively is present in root, stem, leaf and the seed of plant, is one of composition that constitutes in the plant materials in cytolemma, also is the biosynthetic precursor of multiple hormone and steroide.Plant sterol all is widely used in fields such as medicine, makeup, food (comprising inflight meal), feeds.
The source system of plant oil asphalt extracts vegetables oil, as rapeseed oil, soya-bean oil, peanut oil, cottonseed wet goods, finishing operation all carries out hydration degum, the soil of living decolours, the decompression deodorization, and four of alkali-refining deacidification takes off technology and forms soap stock, become the mixed fatty acid of high acid value through acidification, redistillation goes out various lipid acid, and the following clout that obtains is a plant oil asphalt, its boiling point height, dark, the complicated component of color.Wherein contain the plant sterol about 10%, therefore, carry out that the extraction of sterol has important practical significance in the plant oil asphalt.
United States Patent (USP) 3691211 has been reported the method for extracting sterol from Yatall MA pitch, earlier with solvent (ethanol and hydrocarbon) mixture dissolving Yatall MA pitch, add an amount of water again, allow hydrocarbon layer and water layer separate, saponification hydrocarbon layer dissolves at a certain temperature with high molecular weight alcohol or Nitromethane 99Min. and to reclaim sterol.United States Patent (USP) 4524024 has been reported and extracted sterol and lipid acid from Yatall MA pitch, elder generation's hydrolysis Yatall MA pitch, distill out free lipid acid then, obtain being rich in the residue of sterol and sterol ester, with high-molecular weight alcohol dissolution residual substance, filter and remove non-dissolved matter, obtain dissolved sterol phase, steam solvent and obtain sterol.Chinese patent 1807444A has reported and extracted sterol from plant oil asphalt, earlier the free fatty acids in the raw material is converted into fatty acid ester with esterification, obtain being rich in the oil phase of a large amount of sterol esters by washing, by organic solvent the sterol ester alcoholysis in the oil phase is obtained sterol then.But its thick sterol purifying is that treating processes is loaded down with trivial details with water flushing again after methyl alcohol and the water mixture washing, and solvent loss is big.
Summary of the invention
The invention solves above-mentioned the deficiencies in the prior art and problem, a kind of improving one's methods of plant sterol of extracting from plant oil asphalt is provided, this method technology is simple, the product purity height, and product cost is low.
The present invention is achieved by the following technical solutions:
A kind of improving one's methods of plant sterol of extracting from plant oil asphalt of the present invention may further comprise the steps:
(1) under 80～100 ℃ with the plant oil asphalt heat fused, add alkali and water and remain on and constantly stir saponification 0.5 hour under this temperature; Or, under the condition of stirring and refluxing, being heated to 80～100 ℃ with in plant oil asphalt, alkali and the water adding reactor, saponification is 0.5 hour under this temperature and continuous the stirring; Continued heating reflux reaction 1.5～2.5 hours after adding 60～100 ℃ hot water again; The saponification reaction liquid cooling is the back layering but, removes the saponification layer of lower floor; The not saponification layer of collecting gained is added the alcohol of 2～3 times of material asphalt weight, and add alkali, be heated to 75～85 ℃ and refluxed 3～5 hours, stop to heat and stirring; Treat that solution is cooled to the adding of back below 50 ℃ hot water, continues reaction and refluxes 10～30 minutes; Solution is separated out sterol after fully cooling off, and gets the sterol crude product after filtration;
(2) thick sterol organic solvent elution, filtrate steams solvent and puts into drying under 50～60 ℃ of conditions of vacuum drying oven, promptly gets the sterol product.
Of the present inventionly extract improving one's methods of sterol from plant oil asphalt, further technical scheme is that the organic solvent described in its step (2) is alcohol, hexane or acetone.Further technical scheme is that described alcohol is methyl alcohol, ethanol or Virahol again, wherein preferred Virahol.Further technical scheme can also be that described hexane is hexanaphthene or normal hexane again, wherein preferred normal hexane.
Of the present inventionly from plant oil asphalt, extract improving one's methods of sterol, its further technical scheme can also be when using solvent elution sterol crude product in the step (2), solvent load is 5～25 times of sterol crude product quality, and the use temperature of solvent is preferably 25～30 ℃ in its step (2).
A kind of extracting method step of the present invention is as follows:
(1) 30g plant oil asphalt, 12g sodium hydroxide and an amount of water are joined in the reactor that has agitator, reflux exchanger and water-bath, under the condition that stirs and heat, be heated to 95 ℃, reheat 30 minutes; The hot water that adds 95 ℃ of 99g continued the heating reflux reaction mixture 2 hours, stopped reaction; Reactant is fully cooled off, and reactant obtains layering, and the saponification liquor of lower floor is discarded, and the not saponification layer on upper strata is collected and kept somewhere;
(2) unsaponifiables on upper strata and 75g Virahol are imported in the reactor add 9g potassium hydroxide again, continued back flow reaction 4 hours; Cooling back adds 90g hot water when 50 ℃ of temperature, continued reflux 30 minutes, and stopped reaction is poured out reaction solution and left standstill cooling 2～3 days, separates out sterol;
(3) filter with sand core funnel, the sterol crude product acetone elution that obtains, service temperature is 25 ℃, and the amount of acetone is 5 times of sterol crude product quality, and filtrate is collected in elution 3 times, and solvent is steamed back drying in 50～60 ℃ vacuum drying oven, obtains the sterol product.
The invention has the beneficial effects as follows: extracting method and post-processing step are fairly simple, technical process is simple, the recyclable utilization of solvent, and the rate of recovery is high, raw material cheaply is easy to get, generally factory all burns the processing of raw material, and the present invention optimizes post-processing step, and the product purity that obtains is higher; Solvent for use is easy to get, and the toxicity of solvent is little, and selectivity is good, and the loss of solvent is little, and solvent recovering yield reaches 90～96%, and this method makes suitability for industrialized production be achieved, and has a extensive future.
Embodiment
Below by specific embodiment explanation the present invention, but the present invention not merely is defined in these embodiment.
Embodiment 1
The adding of 30g plant oil asphalt is had in the reactor of agitator, reflux exchanger and water-bath, under the condition that stirs and reflux, be heated to 95 ℃, add 12g sodium hydroxide and a spot of water heating saponification 0.5 hour again, the hot water that adds 95 ℃ of 99g, continued reflux 2 hours, stopped reaction cools off reactant the reactant layering under 15 ℃ of temperature.The saponification liquor of lower floor is discarded, and the unsaponifiables on upper strata is kept somewhere, and contains a certain amount of glyceryl ester and lipid acid not by fully saponified, therefore will be separated and collects.
The unsaponifiables on upper strata and the Virahol of 75g are poured in the reactor, add 6g potassium hydroxide, in the extraction system of routine, extract, back flow reaction 4 hours, be cooled to temperature and add the hot water of 80 ℃ of 90g below 50 ℃ the time, continue reflux 30 minutes, and under 15 ℃ of temperature, left standstill cooling 3 days, separate out sterol.
Filter with sand core funnel, get thick sterol, with acetone soln washing three times, service temperature is 27 ℃ again, the amount of acetone is 5 times of thick sterol quality, collect filtrate, steam solvent and put to 50～60 ℃ the vacuum drying oven dryly, obtain 1.3632g sterol product at last, yield 4.54%, the rate of recovery be in the pitch sterol theoretical content 36.9%, fusing point is 126.8～131.9 ℃, solvent recovering rate is 95.8%.
Embodiment 2
The adding of 40g plant oil asphalt is had in the reactor of agitator, reflux exchanger and water-bath, be heated to 95 ℃ and make its fusing, add 16g sodium hydroxide and a spot of hot water, continue reaction 2 hours, stopped reaction, leave standstill cooling, after the layering unsaponifiables on upper strata is collected heating for dissolving, add 100g Virahol and 9g potassium hydroxide, be heated to 80 ℃ of back flow reaction 4 hours, stopped reaction, reaction solution is cooled to 50 ℃ adds 95 ℃ of hot water of 120g, continued back flow reaction 30 minutes, stopped reaction, under 15 ℃ of left and right sides temperature, leave standstill cooling 3 days, separate out sterol.Filter with sand core funnel, get thick sterol, with hexane solution washing three times, service temperature is 28 ℃ again, and consumption is 18 times of thick sterol quality, collect filtrate, steam and put behind the solvent to 50～60 ℃ the vacuum drying oven dryly, obtain 1.0201g sterol product at last, yield 2.55%, fusing point is 128.5～132.6 ℃, and solvent recovering rate is 94.3%.
Embodiment 3
With the 40g plant oil asphalt, 16g sodium hydroxide and a spot of water add and have agitator, in the reactor of reflux exchanger and water-bath, be heated to 95 ℃ and kept saponification reaction 0.5 hour, add 132g hot water again, continuing reaction refluxed 2 hours, in 15 ℃ of left and right sides temperature, leave standstill cooling and find obvious layering after 2.5 hours, discard the saponification liquor of lower floor, collect the unsaponifiables on upper strata, add 100g Virahol and 9g potassium hydroxide, be heated to 83 ℃, reaction refluxed 4 hours, stopped reaction, allow reaction solution be cooled to 50 ℃, add 120g hot water, continue reaction and refluxed stopped reaction 25 minutes, under 15 ℃ of left and right sides temperature, leave standstill cooling 2 days, separate out sterol.Filter with sand core funnel, get thick sterol, with cyclohexane solution washing three times, service temperature is 28 ℃ again, and the hexanaphthene consumption is 18 times of thick sterol quality, collect filtrate, steam and put behind the solvent to 50～60 ℃ the vacuum drying oven dryly, obtain 0.8040g sterol product at last, yield is 2.01%, fusing point is 128.3～132.1 ℃, and solvent recovering rate is 92.7%.
Embodiment 4
The adding of 40g plant oil asphalt is had in the reactor of agitator, reflux exchanger and water-bath, be heated to 95 ℃ and make its fusing, add 16g sodium hydroxide and a spot of hot water, continue reaction 2 hours, stopped reaction, leave standstill cooling, after the layering unsaponifiables on upper strata is collected heating for dissolving, add 100g Virahol and 9g potassium hydroxide, be heated to 80 ℃ of back flow reaction 4 hours, stopped reaction, reaction solution is cooled to 50 ℃ adds 95 ℃ of hot water of 120g, continued back flow reaction 30 minutes, stopped reaction, under 15 ℃ of left and right sides temperature, leave standstill cooling 3 days, separate out sterol.Filter with sand core funnel, get thick sterol, with methanol solution washing three times, service temperature is 28 ℃ again, and consumption is 25 times of thick sterol quality, collect filtrate, steam and put behind the solvent to 50～60 ℃ the vacuum drying oven dryly, obtain 0.5187g sterol product at last, yield 1.30%, fusing point is 128.5～132.6 ℃, and solvent recovering rate is 93.3%.
Embodiment 5
Wash thick sterol with ethanolic soln, service temperature is 29 ℃, and other operations are identical with embodiment 4.Obtain 0.6236g sterol product at last, yield 1.56%.Fusing point is 128.5～132.6 ℃, and solvent recovering rate is 94.8%.
Embodiment 6
The adding of 30g plant oil asphalt is had in the reactor of agitator, reflux exchanger and water-bath, under the condition that stirs and reflux, be heated to 95 ℃, add 12g sodium hydroxide and a spot of water heating saponification 0.5 hour again, the hot water that adds 95 ℃ of 99g, continued reflux 2 hours, stopped reaction cools off reactant the reactant layering under 15 ℃ of temperature.The saponification liquor of lower floor is discarded, and the unsaponifiables on upper strata is kept somewhere, and contains a certain amount of glyceryl ester and lipid acid not by fully saponified, therefore will be separated and collects.
The unsaponifiables on upper strata and the Virahol of 75g are poured in the reactor, add 6g potassium hydroxide, in the extraction system of routine, extract, back flow reaction 4 hours, be cooled to temperature and add the hot water of 80 ℃ of 90g below 50 ℃ the time, continue reflux 30 minutes, and under 15 ℃ of temperature, left standstill cooling 3 days, separate out sterol.
Filter with sand core funnel, get thick sterol, with aqueous isopropanol washing three times, service temperature is 27 ℃ again, and the Virahol consumption is 25 times of thick sterol quality, collect filtrate, steam solvent and put to 50～60 ℃ the vacuum drying oven dryly, obtain 0.5491g sterol product at last, yield is 1.83%, fusing point is 126.8～131.9 ℃, and solvent recovering rate is 90.1%.
Claims (8)
1, a kind ofly extract improving one's methods of sterol from plant oil asphalt, this method may further comprise the steps: (1) with the plant oil asphalt heat fused, adds alkali and water and remains on and constantly stir saponification 0.5 hour under this temperature under 80～100 ℃; Or with in plant oil asphalt, alkali and the water adding reactor, be heated to 80～100 ℃ under the condition of stirring and refluxing, saponification is 0.5 hour under this temperature and continuous the stirring, adds hot water and continues heated and stirred reaction 1.5～2.5 hours, saponification reaction liquid fully cools off the back and removes the saponification layer, the not saponification layer of gained is added Virahol and alkali, and reflux 3～5 hours stops heating and stirring, reaction solution is poured out, fully sterol is separated out in cooling, filter the sterol crude product;
(2) thick sterol organic solvent elution, filtrate steams solvent and puts into drying under 50～60 ℃ of conditions of vacuum drying oven, promptly gets the sterol product.
2, according to claim 1ly from plant oil asphalt, extract improving one's methods of sterol, it is characterized in that the organic solvent described in the step (2) is alcohol, hexane or acetone.
3, according to claim 2ly from plant oil asphalt, extract improving one's methods of sterol, it is characterized in that described alcohol is methyl alcohol, ethanol or Virahol.
4, according to claim 3ly from plant oil asphalt, extract improving one's methods of sterol, it is characterized in that described alcohol is Virahol.
5, according to claim 2ly from plant oil asphalt, extract improving one's methods of sterol, it is characterized in that described hexane is hexanaphthene or normal hexane.
6, according to claim 2ly from plant oil asphalt, extract improving one's methods of sterol, it is characterized in that described hexane is a normal hexane.
7, according to claim 1ly extract improving one's methods of sterol from plant oil asphalt, when it is characterized in that using in the step (2) solvent elution sterol crude product, solvent load is 5～25 times of sterol crude product quality.
8, according to claim 1ly from plant oil asphalt, extract improving one's methods of sterol, it is characterized in that the use temperature of solvent in the step (2) is 25～30 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN2008102362478A CN101412745B (en) | 2008-11-27 | 2008-11-27 | Improved process for extracting sterol from vegetable oil asphalt |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008102362478A CN101412745B (en) | 2008-11-27 | 2008-11-27 | Improved process for extracting sterol from vegetable oil asphalt |
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| Publication Number | Publication Date |
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| CN101412745A true CN101412745A (en) | 2009-04-22 |
| CN101412745B CN101412745B (en) | 2011-09-21 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101942008A (en) * | 2010-08-31 | 2011-01-12 | 东莞市赫尔逊生物科技有限公司 | Process for extracting phytosterol from papermaking wood pulp oil slick pitch |
| CN101607977B (en) * | 2009-06-12 | 2011-06-29 | 天津工业大学 | Method for extracting and purifying natural phytosterol from oil deodorization distillate residual oil and technique thereof |
| CN104498196A (en) * | 2014-11-26 | 2015-04-08 | 辽宁石油化工大学 | Method for reducing acid value of high acid value vegetable pitch |
| CN105001297A (en) * | 2015-08-03 | 2015-10-28 | 刘火成 | Method for extracting phytosterol from plant pitch |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3691211A (en) * | 1970-12-07 | 1972-09-12 | Procter & Gamble | Process for preparing sterols from tall oil pitch |
| CN100334103C (en) * | 2005-09-20 | 2007-08-29 | 南京工业大学 | Method for extracting phytosterol acetate from plant oil asphalt |
| CN100503630C (en) * | 2006-02-07 | 2009-06-24 | 南京工业大学 | Method for extracting plant sterol from plant oil asphalt |
-
2008
- 2008-11-27 CN CN2008102362478A patent/CN101412745B/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101607977B (en) * | 2009-06-12 | 2011-06-29 | 天津工业大学 | Method for extracting and purifying natural phytosterol from oil deodorization distillate residual oil and technique thereof |
| CN101942008A (en) * | 2010-08-31 | 2011-01-12 | 东莞市赫尔逊生物科技有限公司 | Process for extracting phytosterol from papermaking wood pulp oil slick pitch |
| CN101942008B (en) * | 2010-08-31 | 2012-10-03 | 东莞市赫尔逊生物科技有限公司 | Process for extracting phytosterol from papermaking wood pulp oil slick pitch |
| CN104498196A (en) * | 2014-11-26 | 2015-04-08 | 辽宁石油化工大学 | Method for reducing acid value of high acid value vegetable pitch |
| CN104498196B (en) * | 2014-11-26 | 2018-02-02 | 辽宁石油化工大学 | A kind of method for reducing high acid value plant asphalt acid number |
| CN105001297A (en) * | 2015-08-03 | 2015-10-28 | 刘火成 | Method for extracting phytosterol from plant pitch |
| CN105001297B (en) * | 2015-08-03 | 2017-03-08 | 刘火成 | A kind of method extracting plant sterol from plant asphalt |
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| CN101412745B (en) | 2011-09-21 |
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