CN102618383A - Production method and system of deacidification rice bran oil - Google Patents
Production method and system of deacidification rice bran oil Download PDFInfo
- Publication number
- CN102618383A CN102618383A CN2012101152411A CN201210115241A CN102618383A CN 102618383 A CN102618383 A CN 102618383A CN 2012101152411 A CN2012101152411 A CN 2012101152411A CN 201210115241 A CN201210115241 A CN 201210115241A CN 102618383 A CN102618383 A CN 102618383A
- Authority
- CN
- China
- Prior art keywords
- storage tank
- ethanol
- oil
- rice pollard
- depickling
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Liquid Carbonaceous Fuels (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a production method and a system of deacidification rice bran oil. The production method comprises the following steps of: feeding rice bran oil into a heat exchanger, warming, and filtering through a frame filter; feeding the filtered rice bran oil into a cylinder centrifugal extractor, extracting, and separating the rice bran oil from fatty acid to obtain the deacidification rice bran oil and mixed liquor of the fatty acid and ethanol; and feeding the mixed liquor of the fatty acid and the ethanol into an evaporator, separating, feeding ethanol steam into a condenser, condensing the ethanol steam to be liquid, and recycling the ethanol steam as an extracting agent. The system comprises a crude oil storage tank, a pump I, the heat exchanger, the frame filter, a filtered oil storage tank, a pump II, the cylinder centrifugal extractor, a deacidification oil storage tank, a fatty acid and ethanol mixing liquor storage tank, a pump III, the evaporator, a free fatty acid storage tank, the condenser and an ethanol recovery tank. The whole production process is non-toxic and environmental-friendly, the extracting agent ethanol can be recovered and recycled, the production cost is low, the operation process is continuous, the equipment is simple to operate, the operation cost is low, and scale production can be realized.
Description
Technical field
The invention belongs to the vegetable oil refining field, particularly a kind of working method of depickling Rice pollard oil and system.
Background technology
Rice pollard oil is the grease that utilizes paddy processing gained sub product rice bran to produce; 200,000,000 tons of China's paddy annual outputs; 2,000 ten thousand tons in processing gained sub product rice bran can be produced 3,000,000 tons of Rice pollard oils, is widely used in eating, fields such as medicine, chemical industry, foodstuff additive.Mainly contain oleic acid and linolic acid in the edible rice bran oil, also contain thiaminogen, the acid of paddy steroid and vitamin E, the ability reducing cholesterol is prevented and treated cardiovascular disorder, and the treatment nervous system disorders is a kind of nutrient health care edible oil.
Paddy adds man-hour, and rice bran leaves parent paddy and contacts with oxygen, under the effect of lipolytic enzyme; The free fatty acid content of rice bran crude oil rises rapidly; Rice bran crude oil free fatty acid content is 10%～15%, even some is up to 15%～30%, has a strong impact on oil quality and refining yield.
The method of Rice pollard oil depickling at present mainly contains alkali-refining deacidification method, distillation depickling method, esterification deacidification method.The alkali-refining deacidification method is applicable to the Rice pollard oil of free fatty acids low levels, and the Rice pollard oil higher to free fatty acid content needs repeatedly alkali refining, consumes a large amount of alkali lye, and cost increases, and produces great amount of wastewater; The product refining yield is low, and thiaminogen runs off big, and color and luster is dark.Distillation depickling method is strict to the grease pre-treatment, and the higher Rice pollard oil of free fatty acid content needs repeatedly the HTHP distillation, consumes great amount of heat energy, electric energy, and production cost is high, and vitamin E is lost in the free fatty acids; And grease is at high temperature, can produce the material that is harmful to health, the trans fatty acid of generation and propylene chlorohydrin, and edible back suppresses to grow.The esterification deacidification method is to utilize the enzyme catalyst esterification to add glycerol method to reduce grease, but this method esterification temperature is high, add catalyzer after; Can produce a sweet fat, sweet two fat, grease oil has the sex change phenomenon, the unsuitable edible oil of doing; Simultaneously can't carry out scale prodn; And use enzyme to cost an arm and a leg, production cost is high, is not suitable for suitability for industrialized production.
Summary of the invention
The technical problem that the present invention will solve provides a kind of working method and system of simple to operate, the depickling Rice pollard oil that do not need high temperature heat source, and this method need not to use alkali, acid and enzyme catalyst, and production cost is low, and good product quality is fit to suitability for industrialized production.
Technical solution of the present invention is:
A kind of working method of depickling Rice pollard oil, its special character is:
1.1 Rice pollard oil filters
Rice pollard oil gets into interchanger from the crude oil storage tank makes the Rice pollard oil temperature rise to 35 ℃～40 ℃, filters through flame filter press, makes foreign matter content in the Rice pollard oil＜0.2%, sends into the filter oil storage tank;
1.2 extraction depickling
Rice pollard oil in the filter oil storage tank gets into the cylinder centrifugal extractor; And adding ethanol extracts in the cylinder centrifugal extractor; With Rice pollard oil and fatty acid separation, separate the depickling Rice pollard oil that obtains and send into the depickling oil tank, lipid acid and alcohol mixed solution are sent into lipid acid and ethanol mixing storage tank;
Evaporation separates 1.3 free fatty acids is with solvent liquid
Lipid acid in lipid acid and the ethanol mixing storage tank and alcohol mixeding liquid get into vaporizer, separation of fatty acids and ethanol, and lipid acid is sent into the lipid acid storage tank from base of evaporator, and alcohol vapour reclaims from evaporated on top;
1.4 solvent gas condensing and recycling
Alcohol vapour gets into condenser condenses and becomes liquid, gets into the ethanol withdrawing can.
Said flame filter press, filtration medium fineness are 80 orders～100 orders, filter when initial, and the Rice pollard oil gravity flow, when gravity flow was smooth, pressure filtration when the filter internal pressure reaches 0.3MPa, was carried out the slag dumping cleaning.
During extraction, Rice pollard oil and alcoholic acid mass ratio are 1:1～1:3.
The vaporization temperature of said vaporizer is 80 ℃～85 ℃, so that ethanol becomes gas by liquid, and free fatty acids does not evaporate, thereby reaches separation.
A kind of production system of depickling Rice pollard oil, its special character is: comprise the crude oil storage tank, with the interchanger of crude oil storage tank through pipe connection; On the pipeline between crude oil storage tank and the interchanger, be provided with the pump I; The flame filter press that is connected with interchanger, the filter oil storage tank that is connected with flame filter press is with the cylinder centrifugal extractor of filter oil storage tank through pipe connection; Described cylinder centrifugal extractor is respectively equipped with oil inlet, ethanol import, outlet I and outlet II; Between the oil inlet of cylinder centrifugal extractor and filter oil storage tank, be provided with the pump II, the depickling oil tank that is connected with the outlet I and exports lipid acid and the ethanol mixing storage tank that II is connected; With lipid acid and ethanol mixing storage tank vaporizer through pipe connection; Be provided with the pump III on the pipeline between lipid acid and ethanol mixing storage tank and the vaporizer, the free fatty acids storage tank that is connected with vaporizer tower bottom outlet, the condensing surface that is connected with the vaporizer tower top outlet; The ethanol withdrawing can that is connected with condensing surface, described ethanol withdrawing can outlet links to each other with the ethanol import of cylinder centrifugal extractor and forms the closed cycle pipeline.
Pipeline between said crude oil storage tank and the pump I is provided with ball valve, and the pipeline between said filter oil storage tank and the pump II is provided with ball valve.
Said cylinder centrifugal extractor adopts at least three monomer extractors to be in series, and the outlet II of back one-level is that ethanol outlet and enter the mouth with the ethanol of previous stage is connected, thereby reaches continuous production, satisfies the requirement of output and quality.
The present invention utilizes nonesterified fatty acid in ethanol, to be prone to dissolve, and the characteristic of Rice pollard oil indissoluble in ethanol, the promptly similar principle that mixes is separated free fatty acids from Rice pollard oil, thereby reduces the free fatty acid content of Rice pollard oil, and its advantage is:
(1) use ethanol can effectively make rice bran remove free fatty acids as extraction agent, ethanol also has decolorization simultaneously, improves follow-up processing efficiency.
(2) operation of extraction deacidification can accomplish scale production, and operation of equipment is simple continuously, and process cost is low, and oily loss is few, and the Rice pollard oil quality after the depickling is good.
(3) nontoxic, the environmental protection of whole process of production, extraction agent ethanol can be reclaimed repeatedly and used, and production cost is low, and does not need high temperature heat source, and the save energy cost has huge economic and social benefit.
Description of drawings
Fig. 1 is system schematic of the present invention;
Fig. 2 is a process flow sheet of the present invention;
Among the figure: 1-crude oil storage tank, 2-pump I, 3-interchanger, 4-flame filter press, 5-filter oil storage tank, 6-pump II; 7-cylinder centrifugal extractor, 8-depickling oil tank, 9-lipid acid and ethanol mixing storage tank, 10-pump III, 11-vaporizer; 12-free fatty acids storage tank, 13-condensing surface, 14-ethanol withdrawing can, 701-cylinder centrifugal extractor I, 702-cylinder centrifugal extractor II; 703-cylinder centrifugal extractor III, the A-oil inlet, the import of B-ethanol, C-exports I, and D-exports II.
Embodiment
Embodiment 1
As shown in Figure 1, this Rice pollard oil depickling production system comprises crude oil storage tank 1; With the interchanger 3 of crude oil storage tank 1 through pipe connection, the pipeline between crude oil storage tank 1 and interchanger 3 is provided with pump I2, on the pipeline between crude oil storage tank 1 and the pump I 2, is provided with ball valve; The flame filter press 4 that is connected with interchanger 3, the filter oil storage tank 5 that is connected with flame filter press 4 is with the cylinder centrifugal extractor 7 of filtration storage tank 5 through pipe connection; Described cylinder centrifugal extractor 7 is in series by at least three monomer extractors; Present embodiment is an example with three grades of series connection, is respectively cylinder centrifugal extractor I 701, cylinder centrifugal extractor II 702, cylinder centrifugal extractor III 703, and each cylinder centrifugal extractor is respectively equipped with oil inlet A, ethanol import B, outlet I C, outlet II D; Previous stage outlet I C links to each other with back one-level oil inlet A; Back one-level outlet II D links to each other with previous stage ethanol import B, between first step oil inlet A and filter oil storage tank 5, is provided with pump II 6, on the pipeline between filter oil storage tank 5 and the pump II 6, is provided with ball valve; D is connected to lipid acid and ethanol mixing storage tank 9 in first step outlet II; C is connected to depickling oil tank 8 in third stage outlet I, passes through the vaporizer 11 of pipe connection with lipid acid and ethanol mixing storage tank 9, is being provided with pump III 10 on the pipeline between lipid acid and ethanol mixing storage tank 9 and the vaporizer 11; The free fatty acids storage tank 12 that is connected with vaporizer 11 tower bottom outlets; The condensing surface 13 that is connected with vaporizer 11 tower top outlets, the ethanol withdrawing can 14 that is connected with condensing surface 13, described ethanol withdrawing can 14 outlets link to each other with third stage ethanol import B and form the closed cycle pipeline.
As shown in Figure 2, following with the working method concrete steps of that Rice pollard oil depickling:
(1) Rice pollard oil filters
With the free fatty acids mass content is that 15% Rice pollard oil is squeezed in the crude oil storage tank 1, through pump I2 Rice pollard oil is sent into interchanger 3 and makes the Rice pollard oil temperature rise to 35 ℃, and (the filtration medium fineness is 80 orders through flame filter press 4; Filter when initial, the Rice pollard oil gravity flow is when gravity flow is smooth; Pressure filtration when the filter internal pressure reaches 0.3MPa, is carried out the slag dumping cleaning) filter; Foreign matter content is 0.15% in the Rice pollard oil, gets into filter oil storage tank 5;
(2) extraction depickling
Adopt pump II 6 that the flow of the filtration Rice pollard oil in the filter oil storage tank 5 according to 3L/h got in the cylinder centrifugal extractor I 701 through first step oil inlet A; Mix with ethanol and to extract; Lipid acid after the extracting and separating and alcohol mixed solution are sent into lipid acid and the ethanol mixing storage tank 9 from first step outlet II D; The depickling Rice pollard oil gets into the cylinder centrifugal extractor II 702 through second stage oil inlet A from first step outlet I C; Mix with ethanol and to extract; Outlet II D gets into cylinder centrifugal extractor I 701 through first step ethanol import B from the second stage for lipid acid after the extracting and separating and alcohol mixed solution, and the depickling Rice pollard oil gets into the cylinder centrifugal extractor III 703 through third stage oil inlet A from second stage outlet I C, mixes extracting with ethanol; Lipid acid after the extracting and separating and alcohol mixed solution get into cylinder centrifugal extractor II 702 from third stage outlet II D through second stage ethanol import B, and the depickling Rice pollard oil is gone into depickling oil tank 8 from third stage outlet I C;
(3) evaporation separates free fatty acids with solvent liquid
Adopt lipid acid and alcohol mixeding liquid in pump III 10 lipid acid and the ethanol mixing storage tank 9 to get into vaporizer 11; Temperature is 80 ℃～82 ℃ in the vaporizer; Ethanol becomes gas by liquid, and free fatty acids does not evaporate, thereby reaches separation; Lipid acid is sent into lipid acid storage tank 12 at the bottom of vaporizer 11 towers, alcohol vapour reclaims from the cat head evaporation;
(4) solvent gas condensing and recycling
Alcohol vapour gets into condenser condenses 13, and during condensation, the water with 30 ℃ in the condensing surface carries out heat exchange; Water is walked tube side, and alcohol gas is walked shell side, reversed flow condensation; Ethanol becomes liquid by gas; Enter in the ethanol withdrawing can 14, the ethanol of ethanol withdrawing can 14 is got into cylinder centrifugal extractor III 703, a successive round-robin of whole extraction removal process form process according to flow 3L/h through third stage ethanol import B.
Embodiment 2
The working method concrete steps of this Rice pollard oil depickling are following:
(1) Rice pollard oil filters
With the free fatty acids mass content is that 25% Rice pollard oil is squeezed in the crude oil storage tank 1, through pump I2 Rice pollard oil is sent into interchanger 3 and makes the Rice pollard oil temperature rise to 40 ℃, and (the filtration medium fineness is 100 orders through flame filter press 4; Filter when initial, the Rice pollard oil gravity flow is when gravity flow is smooth; Pressure filtration when the filter internal pressure reaches 0.3MPa, is carried out slag dumping cleaning) filter after; Foreign matter content is 0.2% in the Rice pollard oil, gets into filter oil storage tank 5;
(2) extraction depickling
Adopt pump II 6 that the flow of the filtration Rice pollard oil in the filter oil storage tank 5 according to 3L/h got in the cylinder centrifugal extractor I 701 through first step oil inlet A; Mix with ethanol and to extract; Lipid acid after the extracting and separating and alcohol mixed solution are sent into lipid acid and the ethanol mixing storage tank 9 from first step outlet II D; The depickling Rice pollard oil gets into the cylinder centrifugal extractor II 702 through second stage oil inlet A from first step outlet I C; Mix with ethanol and to extract; Outlet II D gets into cylinder centrifugal extractor I 701 through first step ethanol import B from the second stage for lipid acid after the extracting and separating and alcohol mixed solution, and the depickling Rice pollard oil gets into the cylinder centrifugal extractor III 703 through third stage oil inlet A from second stage outlet I C, mixes extracting with ethanol; Lipid acid after the extracting and separating and alcohol mixed solution get into cylinder centrifugal extractor II 702 from third stage outlet II D through second stage ethanol import B, and the depickling Rice pollard oil is gone into depickling oil tank 8 from third stage outlet I C;
(3) evaporation separates free fatty acids with solvent liquid
Adopt lipid acid and alcohol mixeding liquid in pump III 10 lipid acid and the ethanol mixing storage tank 9 to get into vaporizer 11; Temperature is 82 ℃～84 ℃ in the vaporizer; Ethanol becomes gas by liquid, and free fatty acids does not evaporate, thereby reaches separation; Lipid acid is sent into lipid acid storage tank 12 at the bottom of vaporizer 11 towers, alcohol vapour reclaims from the cat head evaporation;
(4) solvent gas condensing and recycling
Alcohol vapour gets into condenser condenses 13, and during condensation, the water with 10 ℃ in the condensing surface carries out heat exchange; Water is walked tube side, and alcohol gas is walked shell side, reversed flow condensation; Ethanol becomes liquid by gas; Enter in the ethanol withdrawing can 14, the ethanol of ethanol withdrawing can 14 is got into cylinder centrifugal extractor III 703, a successive round-robin of whole extraction removal process form process according to flow 9L/h through third stage ethanol import B.
Embodiment 3
The working method concrete steps of this Rice pollard oil depickling are following:
(1) Rice pollard oil filters
With the free fatty acids mass content is that 30% Rice pollard oil is squeezed in the crude oil storage tank 1, through pump I2 Rice pollard oil is sent into interchanger 3 and makes the Rice pollard oil temperature rise to 40 ℃, and (the filtration medium fineness is 90 orders through flame filter press 4; Filter when initial, the Rice pollard oil gravity flow is when gravity flow is smooth; Pressure filtration when the filter internal pressure reaches 0.3MPa, is carried out slag dumping cleaning) filter after; Foreign matter content is 0.17% in the Rice pollard oil, gets into filter oil storage tank 5;
(2) extraction depickling
Adopt pump II 6 that the flow of the filtration Rice pollard oil in the filter oil storage tank 5 according to 3L/h got in the cylinder centrifugal extractor I 701 through first step oil inlet A; Mix with ethanol and to extract; Lipid acid after the extracting and separating and alcohol mixed solution are sent into lipid acid and the ethanol mixing storage tank 9 from first step outlet II D; The depickling Rice pollard oil gets into the cylinder centrifugal extractor II 702 through second stage oil inlet A from first step outlet I C; Mix with ethanol and to extract; Outlet II D gets into cylinder centrifugal extractor I 701 through first step ethanol import B from the second stage for lipid acid after the extracting and separating and alcohol mixed solution, and the depickling Rice pollard oil gets into the cylinder centrifugal extractor III 703 through third stage oil inlet A from second stage outlet I C, mixes extracting with ethanol; Lipid acid after the extracting and separating and alcohol mixed solution get into cylinder centrifugal extractor II 702 from third stage outlet II D through second stage ethanol import B, and the depickling Rice pollard oil is gone into depickling oil tank 8 from third stage outlet I C;
(3) evaporation separates free fatty acids with solvent liquid
Adopt lipid acid and alcohol mixeding liquid in pump III 10 lipid acid and the ethanol mixing storage tank 9 to get into vaporizer 11; Temperature is 83～85 ℃ in the vaporizer; Ethanol becomes gas by liquid, and free fatty acids does not evaporate, thereby reaches separation; Lipid acid is sent into lipid acid storage tank 12 at the bottom of vaporizer 11 towers, alcohol vapour reclaims from the cat head evaporation;
(4) solvent gas condensing and recycling
(4) solvent gas condensing and recycling
Alcohol vapour gets into condenser condenses 13, and during condensation, the water with 15 ℃ in the condensing surface carries out heat exchange; Water is walked tube side, and alcohol gas is walked shell side, reversed flow condensation; Ethanol becomes liquid by gas; Enter in the ethanol withdrawing can 14, the ethanol of ethanol withdrawing can 14 is got into cylinder centrifugal extractor III 703, a successive round-robin of whole extraction removal process form process according to flow 6L/h through third stage ethanol import B.
Detect the index contrast before and after the Rice pollard oil depickling, as shown in table 1:
Table 1
Claims (7)
1. the working method of a depickling Rice pollard oil is characterized in that:
1.1 Rice pollard oil filters
Rice pollard oil gets into interchanger from the crude oil storage tank makes the Rice pollard oil temperature rise to 35 ℃～40 ℃, filters through flame filter press, makes foreign matter content in the Rice pollard oil＜0.2%, sends into the filter oil storage tank;
1.2 extraction depickling
Rice pollard oil in the filter oil storage tank gets into the cylinder centrifugal extractor; And adding ethanol extracts in the cylinder centrifugal extractor; With Rice pollard oil and fatty acid separation, separate the depickling Rice pollard oil that obtains and send into the depickling oil tank, lipid acid and alcohol mixed solution are sent into lipid acid and ethanol mixing storage tank;
Evaporation separates 1.3 free fatty acids is with solvent liquid
Lipid acid in lipid acid and the ethanol mixing storage tank and alcohol mixeding liquid get into vaporizer, separation of fatty acids and ethanol, and lipid acid is sent into the lipid acid storage tank from base of evaporator, and alcohol vapour reclaims from evaporated on top;
1.4 solvent gas condensing and recycling
Alcohol vapour gets into condenser condenses and becomes liquid, gets into the ethanol withdrawing can.
2. the working method of depickling Rice pollard oil according to claim 1 is characterized in that: said flame filter press, filtration medium fineness are 80 orders～100 orders; Filter when initial, the Rice pollard oil gravity flow is when gravity flow is smooth; Pressure filtration when the filter internal pressure reaches 0.3MPa, is carried out the slag dumping cleaning.
3. the working method of depickling Rice pollard oil according to claim 1 is characterized in that: during extraction, Rice pollard oil and alcoholic acid mass ratio are 1:1～1:3.
4. the working method of depickling Rice pollard oil according to claim 1 is characterized in that: the vaporization temperature of said vaporizer is 80 ℃～85 ℃, so that ethanol becomes gas by liquid, and free fatty acids does not evaporate, thereby reaches separation.
5. the production system of a depickling Rice pollard oil is characterized in that: comprise the crude oil storage tank, with the interchanger of crude oil storage tank through pipe connection; On the pipeline between crude oil storage tank and the interchanger, be provided with the pump I; The flame filter press that is connected with interchanger, the filter oil storage tank that is connected with flame filter press is with the cylinder centrifugal extractor of filter oil storage tank through pipe connection; Described cylinder centrifugal extractor is respectively equipped with oil inlet, ethanol import, outlet I and outlet II; Between the oil inlet of cylinder centrifugal extractor and filter oil storage tank, be provided with the pump II, the depickling oil tank that is connected with the outlet I and exports lipid acid and the ethanol mixing storage tank that II is connected; With lipid acid and ethanol mixing storage tank vaporizer through pipe connection; Be provided with the pump III on the pipeline between lipid acid and ethanol mixing storage tank and the vaporizer, the free fatty acids storage tank that is connected with vaporizer tower bottom outlet, the condensing surface that is connected with the vaporizer tower top outlet; The ethanol withdrawing can that is connected with condensing surface, described ethanol withdrawing can outlet links to each other with the ethanol import of cylinder centrifugal extractor and forms the closed cycle pipeline.
6. the production system of depickling Rice pollard oil according to claim 5 is characterized in that: on the pipeline between said crude oil storage tank and the pump I, be respectively equipped with ball valve on the pipeline between said filter oil storage tank and the pump II.
7. the production system of depickling Rice pollard oil according to claim 5; It is characterized in that: said cylinder centrifugal extractor adopts at least three monomer extractors to be in series; The outlet II of back one-level is ethanol outlet and is connected with the ethanol inlet of previous stage; Reach continuous production, satisfy the requirement of output and quality.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201210115241 CN102618383B (en) | 2012-04-19 | 2012-04-19 | Production method and system of deacidification rice bran oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201210115241 CN102618383B (en) | 2012-04-19 | 2012-04-19 | Production method and system of deacidification rice bran oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102618383A true CN102618383A (en) | 2012-08-01 |
| CN102618383B CN102618383B (en) | 2013-05-29 |
Family
ID=46558597
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201210115241 Active CN102618383B (en) | 2012-04-19 | 2012-04-19 | Production method and system of deacidification rice bran oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102618383B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104694251A (en) * | 2015-03-19 | 2015-06-10 | 江南大学 | Enzymic method vegetable oil deacidification method and system |
| CN106967503A (en) * | 2017-05-10 | 2017-07-21 | 国网河南省电力公司电力科学研究院 | A kind of device that low acid number natural esters insulating oil is prepared by extracting alkali-refining process |
| CN111411018A (en) * | 2020-03-23 | 2020-07-14 | 太原理工大学 | Method for converting fatty acid into fatty acid ethyl ester |
| CN112779088A (en) * | 2020-12-19 | 2021-05-11 | 蚌埠市江淮粮油有限公司 | Rice bran oil refining and converting device and converting method thereof |
| CN112795426A (en) * | 2020-12-19 | 2021-05-14 | 蚌埠市江淮粮油有限公司 | Production process method for preparing deacidified rice bran oil by extraction method |
| CN115558546A (en) * | 2021-07-01 | 2023-01-03 | 清华大学 | Shea butter upgrading process |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85100116A (en) * | 1985-04-01 | 1986-08-06 | 清华大学 | From waste water from washing wool, reclaim the centrifugal extracting process of lanolin |
| CN101305974A (en) * | 2008-07-11 | 2008-11-19 | 广东新大地生物科技有限公司 | Camellia oil preparation method for cosmetics |
| CN101343593A (en) * | 2008-09-03 | 2009-01-14 | 北京硕泰生物技术有限责任公司 | Depickling method for rice bran oil with high free fatty acid content |
| CN101984028A (en) * | 2010-10-29 | 2011-03-09 | 湖南农业大学 | High-oryzanol rice bran oil two-phase extraction de-acidification refining technology |
| CN102295986A (en) * | 2011-08-03 | 2011-12-28 | 中南林业科技大学 | Preparation method of rice bran oil with low acid value |
-
2012
- 2012-04-19 CN CN 201210115241 patent/CN102618383B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85100116A (en) * | 1985-04-01 | 1986-08-06 | 清华大学 | From waste water from washing wool, reclaim the centrifugal extracting process of lanolin |
| CN101305974A (en) * | 2008-07-11 | 2008-11-19 | 广东新大地生物科技有限公司 | Camellia oil preparation method for cosmetics |
| CN101343593A (en) * | 2008-09-03 | 2009-01-14 | 北京硕泰生物技术有限责任公司 | Depickling method for rice bran oil with high free fatty acid content |
| CN101984028A (en) * | 2010-10-29 | 2011-03-09 | 湖南农业大学 | High-oryzanol rice bran oil two-phase extraction de-acidification refining technology |
| CN102295986A (en) * | 2011-08-03 | 2011-12-28 | 中南林业科技大学 | Preparation method of rice bran oil with low acid value |
Non-Patent Citations (1)
| Title |
|---|
| 刘晔: "高酸值米糠油萃取脱酸工艺的研究", 《粮油加工与食品机械》, no. 12, 31 December 2005 (2005-12-31) * |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104694251A (en) * | 2015-03-19 | 2015-06-10 | 江南大学 | Enzymic method vegetable oil deacidification method and system |
| CN106967503A (en) * | 2017-05-10 | 2017-07-21 | 国网河南省电力公司电力科学研究院 | A kind of device that low acid number natural esters insulating oil is prepared by extracting alkali-refining process |
| CN106967503B (en) * | 2017-05-10 | 2023-04-11 | 国网河南省电力公司电力科学研究院 | Device for preparing low-acid-value natural ester insulating oil through extraction-alkali refining process |
| CN111411018A (en) * | 2020-03-23 | 2020-07-14 | 太原理工大学 | Method for converting fatty acid into fatty acid ethyl ester |
| CN112779088A (en) * | 2020-12-19 | 2021-05-11 | 蚌埠市江淮粮油有限公司 | Rice bran oil refining and converting device and converting method thereof |
| CN112795426A (en) * | 2020-12-19 | 2021-05-14 | 蚌埠市江淮粮油有限公司 | Production process method for preparing deacidified rice bran oil by extraction method |
| CN112779088B (en) * | 2020-12-19 | 2023-09-15 | 蚌埠市江淮粮油有限公司 | Rice bran oil refining conversion device and rice bran oil refining conversion method |
| CN115558546A (en) * | 2021-07-01 | 2023-01-03 | 清华大学 | Shea butter upgrading process |
| CN115558546B (en) * | 2021-07-01 | 2024-03-12 | 清华大学 | Process for upgrading shea butter |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102618383B (en) | 2013-05-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102618383B (en) | Production method and system of deacidification rice bran oil | |
| CN103320220B (en) | Method for distilling and refining high-grade oil by rice bran oil molecules | |
| CN103289816A (en) | Tea oil processing method and device special for tea oil processing method | |
| CN102060936A (en) | Method for extracting rice bran polysaccharide from sub-critical water | |
| CN104651056A (en) | Method for preparing tea tree flower essential oil | |
| CN111635293A (en) | Sodium methoxide production device and method | |
| CN103361179A (en) | Extraction method of lemongrass essential oil | |
| CN203342432U (en) | Hot reflux alcohol extraction device | |
| CN103897734B (en) | A kind of crude montan wax efficient energy-saving deresination method and device | |
| CN202390424U (en) | Production system for preparing deacidified rice bran oil in extraction method | |
| CN208990273U (en) | A kind of de- front-end volatiles molecular distillation purification anacardol system of cashew nut shell oil ultrasonic wave | |
| CN101684429A (en) | Method of extracting castor oil from castor seed meal | |
| CN103055536A (en) | Heat reflux extraction and concentration equipment | |
| CN101029277A (en) | Method for recovering mixed oil by cottonseed protein extracting process | |
| CN206676100U (en) | A kind of piece-rate system | |
| CN205379681U (en) | Highly enriched extrinsic cycle MVR evaporimeter | |
| CN102876351A (en) | Heating, flashing and separating device | |
| CN100357315C (en) | Method for producing poisonless rape seed concentrate protein from coat removed cold pressed cake of rapeseed | |
| CN202297496U (en) | Heating flash separation device | |
| CN100462425C (en) | Method for leaching grease by isopropyl alcohol | |
| CN102492555B (en) | Method and device for high-efficiency energy-saving desolvation of fossilized animal/plant wax-containing solution | |
| CN101028999B (en) | Method for extracting cottonseed protein and recovering methanol | |
| CN201971810U (en) | Edible oil cake refining and processing equipment | |
| CN102559372A (en) | Ethanol replacement oil preparation method and equipment for ethanol replacement oil preparation method | |
| CN109679679A (en) | A kind of heavy aromatics industrial process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: Three village, 121308 Jinzhou City, Liaoning Province town of five peak building Patentee after: LIAONING WUFENG AGRICULTURAL CO., LTD. Address before: Three village, 121308 Jinzhou City, Liaoning Province town of five peak building Patentee before: Beizhen City Wufeng Rise Industry Processing Co., Ltd. |