CN1931983A - Improved caustic refining process for oil and fat - Google Patents
Improved caustic refining process for oil and fat Download PDFInfo
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- CN1931983A CN1931983A CN 200610140626 CN200610140626A CN1931983A CN 1931983 A CN1931983 A CN 1931983A CN 200610140626 CN200610140626 CN 200610140626 CN 200610140626 A CN200610140626 A CN 200610140626A CN 1931983 A CN1931983 A CN 1931983A
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Abstract
The present invention is improved caustic refining process for oil and fat and has different technological parameters adopted based on the quality of the material oil and fat. By means of controlling the neutralizing reaction temperature and time and controlling the reactant concentration, the present invention has reduced saponification loss of neutral oil, lowered content of hydrated phospholipid in oil product and raised oil product yield. The technological process includes no heating or heating the material oil to 75-90 deg.c, adding phosphoric acid to degum, adding alkali solution in proper concentration for long time deacidification, and final centrifugally separating directly or after heating to certain temperature.
Description
Affiliated technical field
The present invention relates to the food oils manufacture field, be specifically related to a kind of improved chemical method alkali-refining process in the oil and fat refining processing.
Background technology
At present, oil processing industry mostly adopts the chemical method alkali-refining process both at home and abroad.This technological process is such: at first, add acid after stock oil heats to 30 ℃～40 ℃ through the reaction of mixing tank thorough mixing, add a certain proportion of liquid caustic soda then and carry out neutralization reaction, the reaction times was generally about 10 minutes.Oil-alkali mixture of finishing neutralization reaction is warmed up to about 75 ℃, carries out oil-soap separation by taking off the soap whizzer.The shortcoming of this technological process is that the liquid caustic soda consumption is very big, and the refining consumption is high, refining cost height.
Summary of the invention
At above problem, in order to solve the shortcoming and defect of original grease processing technique, technical scheme provided by the invention is:
Stock oil is without heating up or being raised to 75 ℃～90 ℃, the concentration that adds weight of oil 0.03%-0.05% then is that 75% phosphoric acid carries out 10-15 minute the reaction of coming unstuck, then add concentration again and be 15% alkali lye and carry out 20～30 minutes depickling reaction, carry out centrifugation then.The oil product few for phospholipids content, that acid value is higher did not need to heat up before adding phosphoric acid, and only need be warmed up to 75 ℃～90 ℃ before centrifugation; And many for phospholipids content, the oil product that acid value is lower then needed stock oil is warmed up to 75 ℃～90 ℃ before adding phosphoric acid, did not then need to have heated up before centrifugation.
The ratio of the liquid caustic soda that adds depends on the acid value and the excess alkali of oil product, and excess alkali generally is controlled at 20%～25% of theoretical alkali.
Can stir when carrying out alkali reaction, stirring velocity is about 60r/min.
Through centrifugal take off soap after, add 90～100 ℃ of hot water by 10～15% of weight of oil and carry out thorough mixing through the washing mixing tanks, anhydrate then and wash whizzer and wash.Temperature during washing (oily gentle water temperature) can not be lower than 85 ℃; In order to prevent to produce the washing emulsion, can in hot water, add an amount of phosphoric acid or citric acid breakdown of emulsion
The depickling oil of process washing is admitted to and carries out vacuum-drying in the drying chamber, and vacuum drying temperature is controlled at 100～105 ℃, and vacuum degree control is at 98.6kPa.
The present invention is the different technical parameter of quality employing according to stock oil, and emphasis is a temperature and time of controlling neutralization reaction, and control reactive material concentration reduces neutral oil saponification loss, the content of hydrated phospholipid in the reduction oil product, the yield of raising oil product.
The invention has the beneficial effects as follows, reduced the cost of oil and fat refining, reduced the refining consumption of oil and fat refining, and can reduce the content of phosphatide in the oil product, improve the quality of products and stability, also prolonged the shelf-lives of product.
Embodiment
Embodiment 1:
Phospholipids content for crude oil is few, and the oil product that acid value is higher adopts following technology:
Crude oil at first is admitted in the stock oil storage tank temporary, and storage tank is connected with variable-frequency metering take away pump, can regulate the flow of crude oil during production.With crude oil metering take away pump crude oil is squeezed in the acid-respons jar through dual filter then, added the phosphoric acid of a certain proportion of 75% concentration, the ratio that adds phosphoric acid is generally 0.03% of weight of oil.When adding crude oil after the acid through mixing tank, oil and acid are mixed fully, stop reaction and be sent after 10～15 minutes in jar.Mixing oil adds the liquid caustic soda of certain proportion and concentration in the alkali mixing tank, liquid caustic soda is sent into by alkali pump, and the liquid caustic soda in the liquid caustic soda jar is that the liquid caustic soda by original concentration about 30% adds a certain amount of water and is diluted to the dilution alkali that reaches processing requirement about 15%.Be sent to behind the thorough mixing of mixing oil through the alkali mixing tank and reacted in the alkali reaction jar 20～30 minutes.The concentration of liquid caustic soda and the ratio of adding are the keys that influences oil and fat refining rate and processed oil quality.General liquid caustic soda concentration is controlled at about 15%, and the ratio of the liquid caustic soda of adding depends on the acid value and the excess alkali of oil product.Excess alkali generally is controlled at 20%～25% of theoretical alkali.If alkali number is low excessively, soap stock is then hard and fluffy, and phenolphthalein indicator is shown neutral; If alkali number is too high, alkali then takes place analyse effect, cause feed pressure to increase, flow reduces, and difficulty takes place in lock out operation; Have only when alkali number is suitable, the soft cunning of soap stock is obvious alkali reaction to phenolphthalein indicator, and depickling oil is also clear.Directly advance to take off the soap whizzer reaction solution fully is warmed up to 75 ℃～90 ℃ through oil-oil heat exchanger and vapor heat exchanger after the reaction in jar after and take off soap.Wherein oil-oil heat exchanger is that finished product deodorised oil with Workshop Production heats up to crude oil, and purpose is further to recycle thermal source.
Add 90～100 ℃ of hot water by 10～15% of weight of oil and carry out thorough mixing from taking off oil that the soap whizzer comes out, anhydrate then and wash whizzer and wash through the washing mixing tanks.Washing is in order further to remove impurity and the residual soap in deoiling.The washing water of washing should adopt soft water; Temperature during washing (oily gentle water temperature) can not be lower than 85 ℃; In order to prevent to produce the washing emulsion, can in hot water, add an amount of phosphoric acid or citric acid breakdown of emulsion.The depickling oil of process washing is admitted to and carries out vacuum-drying in the drying chamber.Wash qualified depickling oil and generally contain 0.5% moisture, drying process adopts vacuum drying process, and service temperature is controlled at 100～105 ℃, and vacuum degree control is at 98.6kPa.Dried oil is admitted to the further processing of next workshop section or sends into the irrigated area as three grades of oil.
Embodiment 2:
The oil product many for phospholipids content, that acid value is lower, adopt following technology:
Crude oil at first is admitted in the stock oil storage tank temporary, and storage tank is connected with variable-frequency metering take away pump, and pump can be regulated the flow of crude oil.With crude oil metering take away pump crude oil is sent then, crude oil is warmed up to 75 ℃～90 ℃ through oil-oil heat exchanger and vapor heat exchanger earlier, and wherein oil-oil heat exchanger is that finished product deodorised oil with Workshop Production heats up to crude oil, and purpose is further to recycle thermal source.Add the phosphoric acid of sending in proportion by the phosphoric acid volume pump again.The ratio that adds phosphoric acid is generally 0.05% of weight of oil.The crude oil that adds after the acid makes oil and acid be mixed fully in sour mixing tank, and mixing oil is sent in the phosphatase reaction jar and reacts then, and mixing oil stops reaction and is sent after 10～15 minutes in the acid-respons jar.Mixing oil adds the liquid caustic soda of certain proportion and concentration in the alkali mixing tank.Liquid caustic soda is sent into by alkali pump, and the liquid caustic soda in the liquid caustic soda jar is that the liquid caustic soda by original concentration about 30% adds a certain amount of water and is diluted to the dilution alkali that reaches processing requirement about 15%.Be sent to behind the thorough mixing of mixing oil through the alkali mixing tank and reacted in the alkali reaction jar 20～30 minutes.The alkali reaction jar is to be with to stir, and stirring velocity 60r/min stirs and wants strong, to guarantee alkali lye enough dispersity be arranged, and sufficient and oil reacts.The concentration of liquid caustic soda and the ratio of adding are the keys that influences oil and fat refining rate and processed oil quality.General liquid caustic soda concentration is controlled at about 15%, and the ratio of the liquid caustic soda of adding depends on the acid value and the excess alkali of oil product.Excess alkali generally is controlled at 20%～25% of theoretical alkali.If alkali number is low excessively, soap stock is then hard and fluffy, and phenolphthalein indicator is shown neutral; If alkali number is too high, alkali then takes place analyse effect, cause feed pressure to increase, flow reduces, and difficulty takes place in lock out operation; Have only when alkali number is suitable, the soft cunning of soap stock is obvious alkali reaction to phenolphthalein indicator, and depickling oil is also clear.Directly advance to take off the soap whizzer after reaction solution fully reacts and take off soap in jar.When other conditional stabilitys, the separating effect of disc centrifuge can be adjusted by regulating light phase export pressure.When gently containing more soap and water, heavy phase in mutually and contain a small amount of oil (the observed oil of light phase export visor is unintelligible, is muddy shape), can suitably transfer large outlet pressure.Depart to the centre hole outer rim when the separating interface position, accompany morely when oily in the heavy phase, can suitably turn down light phase export pressure.Under normal circumstances, light phase export pressure generally is controlled at 0.1～0.3MPa.Feed pressure depends on flow and light phase export pressure, generally also is controlled at 0.1～0.3MPa.
Add 90～100 ℃ of soft water by 10～15% of weight of oil and carry out thorough mixing from taking off depickling oil that the soap whizzer comes out, anhydrate then and wash whizzer and wash through the washing mixing tanks.Washing is in order further to remove impurity and the residual soap in deoiling.The washing water of washing should adopt soft water; Temperature during washing (oily gentle water temperature) can not be lower than 85 ℃; In order to prevent to produce the washing emulsion, can in hot water, add an amount of phosphoric acid or citric acid breakdown of emulsion.The depickling oil of process washing is admitted to and carries out vacuum-drying in the drying chamber.Wash qualified depickling oil and generally contain 0.5% moisture, drying process adopts vacuum drying process, and service temperature is controlled at 100～105 ℃, and vacuum degree control is at 98.6kPa.Dried oil is admitted to the further processing of next workshop section or sends into the irrigated area as three grades of oil.
Claims (7)
1. oil alkali refining technology, it is characterized in that: stock oil is that 75% phosphoric acid carries out 10-15 minute the reaction of coming unstuck without the direct concentration of adding weight of oil 0.03%-0.05% of just heating up, add concentration again and be about 15% alkali lye and carry out 20～30 minutes depickling reaction, carry out centrifugation after it being warmed up to 75 ℃～90 ℃ again.
2. oil alkali refining technology according to claim 1 is characterized in that: stock oil is warmed up to 75 ℃～90 ℃ earlier, and then after the neutralization reaction of the come unstuck reaction and the adding alkali lye of the above-mentioned adding phosphoric acid of process, directly carries out centrifugation.
3. according to the oil alkali refining technology described in claim 1 or 2, it is characterized in that: the ratio of the liquid caustic soda of adding depends on the acid value and the excess alkali of oil product, and excess alkali generally is controlled at 20%～25% of theoretical alkali.
4. according to the oil alkali refining technology described in the claim 3, it is characterized in that: can stir when carrying out alkali reaction, stirring velocity is about 60r/min.
5. according to the oil alkali refining technology described in the claim 4, it is characterized in that: through centrifugal taking off after the soap, add 90～100 ℃ of hot water by 10～15% of weight of oil and carry out thorough mixing, anhydrate then and wash whizzer and wash through the washing mixing tanks.
6. according to the oil alkali refining technology described in claim 4 or 5, it is characterized in that: be admitted to through the depickling oil of washing again and carry out vacuum-drying in the drying chamber, vacuum drying temperature is controlled at 100～105 ℃, and vacuum degree control is at 98.6kPa
7. according to the oil alkali refining technology described in the claim 5, it is characterized in that: the oily gentle water temperature during washing can not be lower than 85 ℃, adopts soft water, and adds an amount of phosphoric acid or citric acid.
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| Application Number | Priority Date | Filing Date | Title |
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| CN 200610140626 CN1931983A (en) | 2006-09-30 | 2006-09-30 | Improved caustic refining process for oil and fat |
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| CN 200610140626 CN1931983A (en) | 2006-09-30 | 2006-09-30 | Improved caustic refining process for oil and fat |
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| CN1931983A true CN1931983A (en) | 2007-03-21 |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102240016A (en) * | 2011-05-18 | 2011-11-16 | 华南理工大学 | Method for purifying chicken marination processing byproduct chicken oil |
| CN101649252B (en) * | 2009-08-28 | 2012-05-23 | 江苏牧羊迈安德食品机械有限公司 | Alkali-refining process of vegetable oil with high content of unsaturated acid |
| CN104487558A (en) * | 2012-06-14 | 2015-04-01 | 邦吉全球创新有限责任公司 | Process for production of low saturate oils |
| CN106433949A (en) * | 2016-09-09 | 2017-02-22 | 王俊人 | Low-acid-value Yunnan pine seed oil, preparation method and application thereof |
| CN108203619A (en) * | 2016-12-19 | 2018-06-26 | 丰益(上海)生物技术研发中心有限公司 | A kind of sunflower oil for retaining more active nutrient components |
| CN117305016A (en) * | 2023-10-19 | 2023-12-29 | 湖南师范大学 | Refined oil neutralization process optimization control method based on intelligent decision-making mode mining |
-
2006
- 2006-09-30 CN CN 200610140626 patent/CN1931983A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101649252B (en) * | 2009-08-28 | 2012-05-23 | 江苏牧羊迈安德食品机械有限公司 | Alkali-refining process of vegetable oil with high content of unsaturated acid |
| CN102240016A (en) * | 2011-05-18 | 2011-11-16 | 华南理工大学 | Method for purifying chicken marination processing byproduct chicken oil |
| CN104487558A (en) * | 2012-06-14 | 2015-04-01 | 邦吉全球创新有限责任公司 | Process for production of low saturate oils |
| US9657319B2 (en) | 2012-06-14 | 2017-05-23 | Bunge Global Innovation Llc | Process for production of low saturate oils |
| CN104487558B (en) * | 2012-06-14 | 2018-07-17 | 邦吉全球创新有限责任公司 | Method for producing low saturated oils |
| CN106433949A (en) * | 2016-09-09 | 2017-02-22 | 王俊人 | Low-acid-value Yunnan pine seed oil, preparation method and application thereof |
| CN108203619A (en) * | 2016-12-19 | 2018-06-26 | 丰益(上海)生物技术研发中心有限公司 | A kind of sunflower oil for retaining more active nutrient components |
| CN117305016A (en) * | 2023-10-19 | 2023-12-29 | 湖南师范大学 | Refined oil neutralization process optimization control method based on intelligent decision-making mode mining |
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Open date: 20070321 |