CN104312721A - Refining method of rice oil - Google Patents
Refining method of rice oil Download PDFInfo
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- CN104312721A CN104312721A CN201410585558.0A CN201410585558A CN104312721A CN 104312721 A CN104312721 A CN 104312721A CN 201410585558 A CN201410585558 A CN 201410585558A CN 104312721 A CN104312721 A CN 104312721A
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- Prior art keywords
- oil
- refining
- deacidifying
- carry out
- secondarily
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/001—Refining fats or fatty oils by a combination of two or more of the means hereafter
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23D—EDIBLE OILS OR FATS, e.g. MARGARINES, SHORTENINGS, COOKING OILS
- A23D9/00—Other edible oils or fats, e.g. shortenings, cooking oils
- A23D9/02—Other edible oils or fats, e.g. shortenings, cooking oils characterised by the production or working-up
- A23D9/04—Working-up
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/02—Refining fats or fatty oils by chemical reaction
- C11B3/06—Refining fats or fatty oils by chemical reaction with bases
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/16—Refining fats or fatty oils by mechanical means
Abstract
The invention discloses a refining method of rice oil. The refining method comprises the following steps: degumming; primarily decoloring; primarily deacidifying; dewaxing; degreasing; secondarily deacidifying; secondarily decoloring and deodorizing, wherein the degumming step specifically comprises the following steps: carrying out reaction on heated crude oil and phosphoric acid in an acid reaction tank, then, adding alkaline liquor to mix for centrifugal separation, then, adding water to mix for washing centrifugal separation, and finally vacuum-drying; the primarily deacidifying step is physical deacidifying; the secondarily deacidifying step specifically comprises the following steps: quickly mixing heated oil with alkaline liquor for centrifugal separation, then, adding water for washing centrifugal separation, and finally vacuum-drying. According to the method, in the degumming and secondarily deacidifying steps, alkaline liquor is added to remove part of free fatty acids in grease, thus, not only is oryzanol remained, but also part of pigments can be adsorbed. In the degumming, primarily deacidifying and secondarily deacidifying steps, physical refining and chemical refining are organically combined, so that not only is oryzanol remained and the color reduced, but also the product yield is effectively improved.
Description
Technical field
The present invention relates to a kind of edible oil complete processing, especially a kind of method of refining of Rice oil.
Background technology
Rice oil is commonly called as Rice pollard oil, is rolling in the white course of processing by product rice skin that produces and plumule obtains crude oil through extract technology, by the product obtained after further physical refining or chemical refining process by rice.Owing to containing the materials such as vitamin-E, sterol, thiaminogen in Rice oil, so effects such as having the cholesterol removed in blood, reduction blood fat, promotion growth in humans growth planted by this oil, become domestic and international nutrient health oil of generally acknowledging.It will be further appreciated that, rice oil types not only has this characteristic index of thiaminogen, in its crude oil, the content of thiaminogen is about 2.5%, and its lipid acid composition rationally, make it be subject to the extensive concern of countries in the world, become another edible oil after sunflower seed oil, Fructus Maydis oil.
In the current Rice oil course of processing, the method for chemistry or physical refining is generally taked to carry out precision work production.So-called " chemical refining " is in adopting and depickling mode, removes oily free fatty acid, makes the free fatty acids in grease and caustic soda react gained resultant and be soap stock, utilizes that soap stock is different from the proportion of grease to be separated oil with soap stock.The soap that neutralization generates is surfactant, and adsorptive power is very strong, and other impurity in adsorbable oil, as pigment, suspended substance etc., plays many-sided effects such as depickling, removing impurities, decolouring simultaneously; But in caustic soda and while free fatty acids, also may there is the saponification of sweet three esters, cause the increase of refining consumption." physical refining " is the process that lipid acid becomes gas evaporation under high temperature high vacuum and water vapor exist, and is called physical deacidification; The color of physical deacidification gained oil product cannot reach the accreditation of international customers.
Adopt traditional chemical refining technique, a large amount of soap stocks can be produced, not single yield that can reduce finished product, and the characteristic nutrient substance thiaminogen in Rice oil can lose greatly, run off in soap stock, cause the thiaminogen content in finished product Rice oil low, lose characteristic nutrient substance.Physical refining can be divided into again conventional physical refining and emerging small molecules distillatory refining technology, although these two kinds of technology make thiaminogen nutritive substance be retained, and all Shortcomings parts.Conventional physical underrefining part is: energy consumption is high, easily produces trans fatty acid simultaneously, have potential hazard to HUMAN HEALTH in long pyroprocess.Emerging small molecules distillation technique weak point is: equipment investment cost is high, production capacity is low, and in oil product, benzopyrene content is but not easily rejected, and benzopyrene is strong carcinogen, serious threat HUMAN HEALTH.
Summary of the invention
The technical problem to be solved in the present invention is to provide the method for refining of the high Rice oil of a kind of quality product.
For solving the problems of the technologies described above, the technical solution used in the present invention is: it comprise come unstuck, once decolouring, a depickling, dewaxing, degreasing, secondary depickling, secondary decolourization and deodorization procedures, described Degumming Procedures: crude oil heats afterwards and phosphoric acid reacts in acid-respons tank, then centrifugation is carried out after adding buck mixing, add water again after mixing and carry out washing centrifugation, finally carry out vacuum-drying;
A described deacidification process adopts physical deacidification;
Described secondary deacidification process: carry out centrifugation after oil plant heats and after buck short mix, then add water and carry out washing centrifugation, finally carry out vacuum-drying.
In Degumming Procedures of the present invention, phosphoric acid concentration is 85wt%, addition is quality of crude oil 0.7 ~ 1 ‰; Concentration of lye is 10 degree Beaume.
In Degumming Procedures of the present invention, crude oil Heating temperature to 65 DEG C.
In secondary deacidification process of the present invention, oil plant Heating temperature to 90 DEG C, concentration of lye is 12 ~ 15 degree Beaume.
A deacidification process of the present invention: oil plant enters in extracting tower after being heated to 230 ~ 240 DEG C, depickling under the condition of residual voltage 200Pa.
A bleaching process of the present invention adopts carclazyte decolouring, and secondary decolourization operation adopts carclazyte+gac mixing decolouring.
The beneficial effect adopting technique scheme to produce is: the present invention adds alkali lye to remove part free fatty acids in grease, instead of in picture traditional chemical refining technique, add after link of coming unstuck excess alkali carry out in and depickling.Thiaminogen can be made like this to retain the effect playing again absorbed portion pigment, for physical refining deacidification provides precondition.The present invention coming unstuck, a depickling, physical refining and chemical refining to be organically combined in secondary depickling three operations, thus both remained thiaminogen, reduced color, effectively carried high product yield simultaneously.
The present invention's twice bleaching process is respectively coming unstuck, carry out after secondary depickling, and this use can saving discoloring agent, reduces auxiliary material and add cost, reduces discoloring agent band oil mass, has both improve product yield, and can reduce production cost again.
The present invention adopts twice decolouring scheme at bleaching process, and discoloring agent adopts various combination, both serves decolorization, plays again the effect rejected by benzopyrene in grease.
In sum, physical refining combines with chemical refining by the present invention, make the basis of the maximum reservation of nutrition content in oil product (especially ensures that refining Rice oil two-story valley dimension cellulose content is at more than 8000ppm), reduce east of oil, acid value, elimination benzopyrene, oil quality is met international standards; Present invention process is reasonable, easy to operate, result of use is good.
Accompanying drawing explanation
Below in conjunction with the drawings and specific embodiments, the present invention is further detailed explanation.
Fig. 1 is process flow diagram of the present invention.
Embodiment
Shown in Fig. 1, the method for refining of this Rice oil, the crude oil oil plant of Rice oil enter successively come unstuck, once decolouring, a depickling, dewaxing, degreasing, secondary depickling, secondary decolourization and deodorization procedures, finally obtain refining Rice oil; The concrete technology of each operation is as described below.
1, Degumming Procedures:
After crude oil is heated to 65 DEG C, add quality of crude oil 0.7 ~ 1 ‰, phosphoric acid that concentration is 85wt% mixes, then be delivered in acid-respons tank, the oil adding phosphoric acid stopped after 35 ~ 40 minutes in acid-respons tank, to add water and the alkali lye short mix of 10 degree Beaume is delivered to whizzer and carried out centrifugation, the short mix that adds water after oil after centrifugation sequentially heats is delivered to second, the 3rd bench centrifuge carries out washing centrifugation, delivers to drying tower carry out the qualified degummed oil of dry output quality through the oil of twice washing centrifugation.Wherein, in the oil product after the separation of First centrifuge, thiaminogen controls at 19000 ~ 20000ppm; Oil product acid value after First centrifuge is separated controls at 14 ~ 16KOHmg/kg; Before entering whizzer, oil product is heated to respectively: 85 DEG C, 90 DEG C, 90 DEG C; Before entering drying tower, oil product is heated to 105 DEG C; Drying tower vacuum is-0.085MPa.
2, a bleaching process:
Mix with carclazyte after the degummed oil of upper step gained is heated to 110 DEG C, carclazyte addition is 2 ~ 5% of oil quality; Then bleaching tower decolouring is entered.After oily earth mixtures mixes 40 minutes in bleaching tower, be delivered to filter and filter, the edible vegetable oil (bleached oil) after filtration is delivered in deaerator through security filter, and deoxidation obtains bleached oil.Bleached oil east of oil controls to (cell 25.4mm): Y35, R5.0.
3, a deacidification process:
The bleached oil of upper step gained is delivered to extracting tower after being heated to 230 ~ 240 DEG C, stops in tower and carry out physical deacidification.Extracting tower vacuum is: McLeod vacuum gauge display 200Pa; The oil product residence time in extracting tower: 5 minutes; Depickling oleic acid valency controls extremely: 2 ~ 3KOHmg/kg.
4, dewaxing, degreasing process
The depickling oil of upper step gained is cooled, then delivers to crystallizer and carry out crystallization, growing the grain according to falling temperature gradient.Be delivered to plate-and-frame filter press after growing the grain completes to carry out wax and be separated with oil filtration; Be delivered to after isolated pressed oil heats in degreasing crystallizer and carry out crystallization, growing the grain according to falling temperature gradient.Be delivered to plate-and-frame filter press after growing the grain completes to carry out fat and be separated with oil filtration.
The falling temperature gradient of described dewaxing operation: when 80 ~ 40 DEG C, per hourly fall 5 DEG C; When 40 ~ 30 DEG C, per hourly fall 2 DEG C; When 30 ~ 18 DEG C, per hourly fall 1 DEG C.The rearing crystal time of dewaxing operation is: 8 ~ 12 hours.
Described degreasing process: carry out gradient cooling after pressed oil is heated to 45 DEG C; Gradient cooling is: when 45 ~ 30 DEG C, per hourly fall 3 DEG C; When 30 ~ 20 DEG C, per hourly fall 1.5 DEG C; When 20 ~ 15 DEG C, per hourly fall 1 DEG C; When 15 ~ 8 DEG C, per hourly fall 0.75 DEG C; When 8 ~ 2 DEG C, per hourly fall 0.5 DEG C; Rearing crystal time is: 12 hours.
5, secondary deacidification process:
After the degreasing oil of upper step gained is heated to 90 DEG C, to add water and the alkali lye short mix of 12 ~ 15 degree Beaume is delivered to whizzer and carried out centrifugation, the short mix that adds water after oil after centrifugation sequentially heats is delivered to second, the 3rd bench centrifuge carries out washing centrifugation, delivers to drying tower carry out the qualified secondary depickling oil of dry output quality through the oil of twice washing centrifugation.In oil product after described First centrifuge is separated, thiaminogen controls to 12000ppm, and the oil product acid value after First centrifuge is separated controls to 0.6 ~ 0.8KOHmg/kg; Before entering whizzer, oil product is heated to respectively: 85 DEG C, 90 DEG C, 90 DEG C; Before entering drying tower, oil product is heated to 105 DEG C, and drying tower vacuum is :-0.085MPa.
6, secondary decolourization operation:
Mix with carclazyte+gac after the secondary depickling oil of upper step gained is heated to 110 DEG C, carclazyte+gac (carclazyte: gac=10:1 weight) addition is 5 ~ 6 % of oil quality, then enters bleaching tower decolouring.After oily earth mixtures mixes 35 minutes in bleaching tower, be delivered to filter and filter, the edible vegetable oil (bleached oil) after filtration is delivered in deaerator through security filter.Described secondary decolourization oil colours pool controls to (cell 133.4mm): Y30, R4.0.
7, deodorization procedures:
The secondary decolourization oil of upper step gained is heated to 245 ~ 260 DEG C be delivered to deodorizing tower and carry out deodorization, after deodorised oil cooling, is delivered to product tank.Deodorizing tower vacuum is 100Pa(McLeod vacuum gauge), in deodorizing tower, the oil product residence time is 60 ~ 90 minutes, and after deodorised oil cooling, temperature is 25 ~ 30 DEG C; Processed oil acid value controls to 0.4 ~ 0.5KOHmg/kg, processed oil thiaminogen content >=8000ppm, processed oil color and luster (cell 133.4mm): Y30, R3.0 ~ 3.5.
To sum up: the more traditional refinery practice difference of this technique is mainly:
1. be all add alkali lye to remove part free fatty acids in grease coming unstuck in link and secondary depickling link, instead of in traditional chemical refining technique, add after link of coming unstuck excess alkali carry out in and depickling.Thiaminogen can be made like this to retain the effect playing again absorbed portion pigment, for physical refining deacidification provides precondition.The control that this processing parameter and auxiliary material add, is combined physical refining with chemical refining organic phase in " come unstuck, depickling, secondary depickling " three links.Finally reach: namely remain thiaminogen, reduce color, carry high product yield simultaneously and create organic conditions.
2., in decolouring link, adopt scheme of decolouring for twice, and discoloring agent adopts various combination, namely serves decolorization, play again the effect rejected by benzopyrene in grease.
Twice decolouring link is all carried out after " come unstuck, secondary depickling ", and this technological design, can save the use of discoloring agent, and auxiliary material interpolation cost reduces thereupon, and discoloring agent band oil mass also reduces thereupon, namely improves product yield, can reduce production cost again.
Claims (6)
1. the method for refining of a Rice oil, it comprise come unstuck, once decolouring, a depickling, dewaxing, degreasing, secondary depickling, secondary decolourization and deodorization procedures, it is characterized in that, described Degumming Procedures: crude oil heats afterwards and phosphoric acid reacts in acid-respons tank, then centrifugation is carried out after adding buck mixing, add water again after mixing and carry out washing centrifugation, finally carry out vacuum-drying;
A described deacidification process adopts physical deacidification;
Described secondary deacidification process: carry out centrifugation after oil plant heats and after buck short mix, then add water and carry out washing centrifugation, finally carry out vacuum-drying.
2. the method for refining of a kind of Rice oil according to claim 1, is characterized in that: in described Degumming Procedures, and phosphoric acid concentration is 85wt%, addition is quality of crude oil 0.7 ~ 1 ‰; Concentration of lye is 10 degree Beaume.
3. the method for refining of a kind of Rice oil according to claim 1, is characterized in that: in described Degumming Procedures, crude oil Heating temperature to 65 DEG C.
4. the method for refining of a kind of Rice oil according to claim 1, is characterized in that: in described secondary deacidification process, oil plant Heating temperature to 90 DEG C, and concentration of lye is 12 ~ 15 degree Beaume.
5. the method for refining of a kind of Rice oil according to claim 1, is characterized in that, a described deacidification process: oil plant enters in extracting tower after being heated to 230 ~ 240 DEG C, depickling under the condition of residual voltage 200Pa.
6. the method for refining of a kind of Rice oil according to claim 1-5 any one, is characterized in that: a described bleaching process adopts carclazyte decolouring, and secondary decolourization operation adopts carclazyte+gac mixing decolouring.
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| CN201410585558.0A CN104312721A (en) | 2014-10-28 | 2014-10-28 | Refining method of rice oil |
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| CN201410585558.0A CN104312721A (en) | 2014-10-28 | 2014-10-28 | Refining method of rice oil |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104611132A (en) * | 2015-02-04 | 2015-05-13 | 蚌埠市江淮粮油有限公司 | Acid reducing process of rice oil |
| CN106167738A (en) * | 2016-09-21 | 2016-11-30 | 山东健源油脂科技有限公司 | The rice essential smelting method of high plant sterol |
| CN106749480A (en) * | 2017-02-10 | 2017-05-31 | 山东三星玉米产业科技有限公司 | Oryzanol extracting method in Rice oil |
| CN110903893A (en) * | 2019-12-11 | 2020-03-24 | 江西省金泰粮油食品有限公司 | Deacidification method of edible palm oil |
| CN111394172A (en) * | 2019-01-03 | 2020-07-10 | 江苏康之源粮油有限公司 | Physical distillation-chemical alkali refining combined deacidification process for rice oil |
| CN111394171A (en) * | 2019-01-03 | 2020-07-10 | 江苏康之源粮油有限公司 | Novel composite solvent low-temperature extraction process for rice oil |
| CN111635819A (en) * | 2020-05-11 | 2020-09-08 | 益海（连云港）粮油工业有限公司 | Crude oil refining heat energy comprehensive utilization system |
| CN113122386A (en) * | 2019-12-30 | 2021-07-16 | 丰益(上海)生物技术研发中心有限公司 | Rice oil and preparation method thereof |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104611132A (en) * | 2015-02-04 | 2015-05-13 | 蚌埠市江淮粮油有限公司 | Acid reducing process of rice oil |
| CN106167738A (en) * | 2016-09-21 | 2016-11-30 | 山东健源油脂科技有限公司 | The rice essential smelting method of high plant sterol |
| CN106167738B (en) * | 2016-09-21 | 2019-07-19 | 山东健源油脂科技有限公司 | The rice essential smelting method of high phytosterol |
| CN106749480A (en) * | 2017-02-10 | 2017-05-31 | 山东三星玉米产业科技有限公司 | Oryzanol extracting method in Rice oil |
| CN111394172A (en) * | 2019-01-03 | 2020-07-10 | 江苏康之源粮油有限公司 | Physical distillation-chemical alkali refining combined deacidification process for rice oil |
| CN111394171A (en) * | 2019-01-03 | 2020-07-10 | 江苏康之源粮油有限公司 | Novel composite solvent low-temperature extraction process for rice oil |
| CN110903893A (en) * | 2019-12-11 | 2020-03-24 | 江西省金泰粮油食品有限公司 | Deacidification method of edible palm oil |
| CN113122386A (en) * | 2019-12-30 | 2021-07-16 | 丰益(上海)生物技术研发中心有限公司 | Rice oil and preparation method thereof |
| CN113122386B (en) * | 2019-12-30 | 2023-11-24 | 丰益(上海)生物技术研发中心有限公司 | Rice oil and preparation method thereof |
| CN111635819A (en) * | 2020-05-11 | 2020-09-08 | 益海（连云港）粮油工业有限公司 | Crude oil refining heat energy comprehensive utilization system |
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