CN110540898A - Tea seed oil finish machining process - Google Patents
Tea seed oil finish machining process Download PDFInfo
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- CN110540898A CN110540898A CN201910771984.6A CN201910771984A CN110540898A CN 110540898 A CN110540898 A CN 110540898A CN 201910771984 A CN201910771984 A CN 201910771984A CN 110540898 A CN110540898 A CN 110540898A
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- 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
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- 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
- C11B3/008—Refining fats or fatty oils by filtration, e.g. including ultra filtration, dialysis
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- 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
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- 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
- C11B3/04—Refining fats or fatty oils by chemical reaction with acids
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- 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
- C11B3/10—Refining fats or fatty oils by adsorption
-
- 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
- C11B3/12—Refining fats or fatty oils by distillation
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- 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
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- 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
- C11B7/00—Separation of mixtures of fats or fatty oils into their constituents, e.g. saturated oils from unsaturated oils
- C11B7/0075—Separation of mixtures of fats or fatty oils into their constituents, e.g. saturated oils from unsaturated oils by differences of melting or solidifying points
Abstract
The invention relates to the technical field of tea seed oil processing, in particular to a tea seed oil fine processing technology, which comprises the steps of firstly utilizing phosphoric acid to react with non-hydrated phospholipid in crude oil, utilizing liquid caustic soda to perform neutralization reaction with free fatty acid in the crude oil to generate soap, then settling and separating to achieve the purpose of removing phospholipid, free fatty acid and metal ions in the crude oil, and then washing residual soapstock in oil by hot water; under the vacuum state, removing water in the water washing oil, adding white soil and mixing with the oil to be decolored to achieve the purposes of decoloring and adsorbing impurities; then, filtering the waste argil in the oil by using a leaf filter; then destroying the thermal-sensitive pigment in a high-temperature and high-vacuum environment, removing residual substances influencing the flavor, simultaneously recovering fatty acid, filtering out the wax separated out from the oil by means of cooling and filtering the oil product after renting to obtain the finished oil, thus the fine processing can improve the oil yield and the tea oil quality.
Description
Technical Field
The invention relates to the technical field of tea seed oil processing, in particular to a tea seed oil finish machining process.
Background
tea seed oil, also called camellia oil, is obtained from seeds of camellia oleifera trees, is one of the oldest woody plant oils in China, is mainly composed of unsaturated fatty acids such as oleic acid, linoleic acid, palmitic acid and linolenic acid, is very similar to the composition of olive oil, which is a high-quality plant oil recognized in the world, and has unsaturated fatty acid content higher than that of olive oil, and the physicochemical properties of the tea seed oil are also very similar to those of the olive oil. The conventional oil pressing treatment method is completed by the process steps of artificial drying, natural airing, machine squeezing and the like, and although a better oil yield can be achieved according to the improvement of the quality of each process, the oil yield of the oil tea fruits cannot be stably improved to a greater extent, and the oil tea fruit resources cannot be utilized to a greater extent.
aiming at the defects of the traditional oil pressing technology, the prior art mainly comprises a mechanical hot pressing extraction method and a cold pressing method, the hot pressing method has more equipment and high oil residue rate, active substances such as vitamins and the like are easily damaged due to the traditional high-temperature hot pressing of tea oil, and the extraction method adopts solvent for extraction, so that although the cost is low, the potential safety hazard exists in the tea oil due to the addition of the solvent, and the tea oil is not green; in addition, the refining treatment process in the tea oil processing process has high requirements, and the refining process is also focused, so that the quality of the tea oil prepared from the camellia seeds is still poor, the ideal requirements cannot be met, and the content of the nutritional ingredients of the camellia is still poor.
disclosure of Invention
the invention aims to provide a tea seed oil fine processing technology which has the characteristics of improving the oil yield and the quality of tea seed oil.
In order to solve the technical problem, the invention provides a tea seed oil finishing process, which comprises the following steps:
a. Acidifying, neutralizing and washing, namely converting non-hydrated phospholipid into hydrated phospholipid by utilizing the reaction of phosphoric acid and non-hydrated phospholipid in the crude oil to form a hydrated phospholipid group which is easy to separate; performing neutralization reaction by using liquid alkali and free fatty acid in the crude oil to generate soap, then performing settling separation to achieve the purpose of removing phospholipid, free fatty acid and metal ions in the crude oil, and washing residual soapstock in the oil by hot water;
b. Drying and decoloring, removing water in the water-washed oil in a vacuum state, adding white soil to be mixed with the oil to be decolored, and adsorbing pigments, residual soapstock, phospholipid, metal ions and the like in the crude oil by using argil in the vacuum state so as to achieve the purposes of decoloring and adsorbing impurities;
c. Filtering, namely filtering waste argil in the oil by using a blade filter, and physically deacidifying and deodorizing the filtered decolored oil in a deodorizing pot;
d. Deodorizing, namely destroying the thermal-sensitive pigment in a high-temperature and high-vacuum environment, removing residual substances influencing the flavor, and simultaneously recovering fatty acid to improve the edible quality of the oil product;
e. Dewaxing, namely cooling the oil product, crystallizing and separating out wax with low melting point in the oil from the oil, and filtering out the wax separated out from the oil by a filtering means to obtain the finished oil.
further preferably, in the step a, 10BC '-16 BC' concentration alkali liquor and 70-85% phosphoric acid are prepared in the high-level alkali liquor tank, and the temperature of hot water is 90-100 degrees.
More preferably, in the step a, the acid adding amount is controlled to be 0.05-0.2% of the oil amount; adding and rapidly stirring, controlling the temperature of oil at 60-65 ℃, reacting phosphoric acid for 40 minutes, adding prepared hot water into the oil, adding the hot water within 5 minutes, wherein the amount of the heated water is about 5-10% of the oil amount, reducing the speed to half of the original speed after adding, continuously stirring for about 20 minutes, and standing for about 2-3 hours when oil foot particles are separated out.
Preferably, in the step b, the oil temperature is adjusted to 100-105 ℃, the vacuum degree is adjusted to 85-95KPa, the dehydration is carried out for 60 minutes, the water and the air are completely removed, 1-3% of white clay is added into the dried oil, the mixture is fully stirred and mixed, the oil temperature is kept at 105-120 ℃, the decolorization is carried out for about 30 minutes under the condition of residual pressure of 8KPa, and the mixture is cooled to about 70 ℃ and then is filtered out by a vibration filter through a decolorization pump.
Further preferably, in the step c, after the decolorization is finished, the steam valve is closed, and the oil temperature is reduced to below 70 ℃ for filtration.
Preferably, in the step d, after the temperature of the oil in the deodorization pot reaches 120 ℃, direct superheated steam is introduced to roll the crude oil, and the pressure of the superheated steam entering the deodorization pot cannot be too high, so that the deodorization oil is not too much rolled; stopping heating when the oil temperature is increased to about 230-240 ℃, then starting heat preservation, keeping a vacuum state, continuously communicating direct superheated steam for deodorization for 3 hours, closing a heat conduction oil inlet and outlet valve 30 minutes before deodorization is stopped, closing the direct steam valve after deodorization is finished, starting a deodorization oil pump, opening a deodorization pot and a cooling water inlet and outlet valve of a spiral plate heat exchanger, and pumping a finished oil product to a finished oil tank by using the deodorization oil pump when the oil temperature is reduced to below 50 ℃.
Preferably, in the step e, when the temperature of the oil product is reduced to below 40 ℃, the temperature of the oil product is reduced to 10 ℃ according to the temperature reduction of 3 ℃ per hour, when the temperature of the oil product is reduced to below 10 ℃, the temperature of the oil product is reduced to 6 ℃ according to the temperature reduction of 0.5 ℃ per hour, the oil temperature is kept at about 6 ℃ finally, crystallization and crystal growth are carried out for 6 hours, then filtration is started, and during the cooling period of the crystallization and crystal growth, the rotation speed is required to be controlled to be 8-15 revolutions per minute.
The invention has the beneficial effects that: the invention firstly utilizes the reaction of non-hydrated phospholipid in phosphoric acid and crude oil, and utilizes liquid alkali and free fatty acid in the crude oil to carry out neutralization reaction to generate soap, then the soap is settled and separated, the purpose of removing phospholipid, free fatty acid and metal ions in the crude oil is achieved, and then the residual soapstock in the oil is washed by hot water; under the vacuum state, removing water in the washing oil, adding white soil and mixing with the oil to be decolored to achieve the purposes of decoloring and adsorbing impurities; then, filtering the waste argil in the oil by using a leaf filter; then, the thermosensitive pigment is destroyed in a high-temperature and high-vacuum environment, substances which influence the flavor and are remained are removed, meanwhile, the fatty acid is recovered, and after renting, the wax separated out from the oil is filtered out by means of cooling and filtering the oil product to obtain the finished oil, so that the oil yield and the tea oil quality can be improved by fine processing.
Detailed Description
The present invention will be described in further detail with reference to examples.
Example one
A tea seed oil finish machining process is characterized in that: the method comprises the following steps:
a. acidifying, neutralizing and washing, namely converting non-hydrated phospholipid into hydrated phospholipid by utilizing the reaction of phosphoric acid and non-hydrated phospholipid in the crude oil to form a hydrated phospholipid group which is easy to separate; neutralizing free fatty acid in liquid alkali and crude oil to generate soap, settling, separating to remove phospholipid, free fatty acid and metal ions, washing with hot water to remove residual soapstock,
b. drying and decoloring, removing water in the water washing oil in a vacuum state, adding white soil to be mixed with the oil to be decolored, and adsorbing pigment, residual nigre, phospholipid, metal ions and the like in the crude oil by using argil in the vacuum state so as to achieve the purposes of decoloring and adsorbing impurities;
c. filtering, namely filtering waste argil in the oil by using a blade filter, and physically deacidifying and deodorizing the filtered decolored oil in a deodorizing pot;
d. Deodorizing, namely destroying the thermal-sensitive pigment in a high-temperature and high-vacuum environment, removing residual substances influencing the flavor, and simultaneously recovering fatty acid to improve the edible quality of the oil product;
e. Dewaxing, namely cooling the oil product, crystallizing and separating out wax with low melting point in the oil from the oil, and filtering out the wax separated out from the oil by a filtering means to obtain the finished oil.
In the step a, the lye with the concentration of 10 BC' and the phosphoric acid with the concentration of 85% are prepared in the high-level lye tank, and the temperature of the hot water is 100 degrees.
In the step a, the acid adding amount is controlled to be 0.2 percent of the oil amount; adding and rapidly stirring, controlling the oil temperature at 65 ℃, reacting phosphoric acid for 40 minutes, adding prepared hot water into the oil, finishing adding the hot water within 5 minutes, wherein the heating water amount is about 10 percent of the oil amount, reducing the speed to half of the original speed after adding, continuously stirring for about 20 minutes, standing for about 2-3 hours when oil residue particles are separated out, and condensing the oil residue into large particles to settle at the bottom of a water washing pot. Opening an emptying valve at the bottom of the oil refining pot, putting lower wastewater into an oil separating box, discharging the wastewater separated by the oil separating box into a wastewater pool, pumping the waste oil separated from the oil separating box into the oil refining pot by a pump for recycling, and pumping lower-layer oil residue in the oil refining pot into a soapstock pot by a gear pump after the wastewater is discharged. The two oil refining pots are circularly and alternately used according to the first-in first-out principle. Opening an alkali liquor filling valve, adding a prepared alkali liquor, calculating the alkali addition amount according to the actual acid value of the crude oil according to a formula [ theoretical alkali amount (t) ═ 7.13 multiplied by 10-4 multiplied by oil weight multiplied by acid value ], determining the excess alkali of 0.25 percent of the theoretical alkali oil weight, completing the addition of all the alkali liquor once within 5-10 minutes, simultaneously stirring rapidly (about 60 r/min), not raising the temperature immediately after the alkali addition is completed, and continuing to stir slowly for about 20-30 minutes to ensure that the alkali liquor and the acid in the oil fully react;
After the neutralization reaction is finished, the stirring speed of the oil refining kettle is slowed down (about 30 r/min), then the indirect steam is started to heat the oil, the oil is heated to 80 ℃, the heating is stopped, the heat preservation is started, the temperature is kept at 80 ℃ all the time, the stirring is continued for about 10min to promote the coagulation of the nigre, and the stirring is stopped when the oil and the nigre are in a separated state. The stirring speed should be reduced to about 30 rpm during the temperature rise process to prevent the soap particles from being broken up. After reaching the final temperature, the soapstock and the oil easily separate and sink quickly.
If the soapstock is sticky and in a more permanent suspension state in the production process, clear water or diluted saline water which is at the same temperature as or slightly higher than the oil temperature can be added, and the pressure water is called as pressurized water. Promoting the specific gravity of the soap particles to increase and sink after absorbing water. The water amount is 10%, and after stirring is stopped, the mixture is kept still for 3-4 hours. Opening an emptying valve at the bottom of the oil refining pot, pumping soapstock at the bottom of the oil refining pot into the soapstock pot by using a gear pump, wherein the soapstock discharge condition is observed, and the emptying valve is closed in time when oil is discharged; if necessary, carrying out secondary alkali refining, and if the soap grains are too large, increasing the neutral oil content of soapstock and not reducing the stirring speed in the temperature rising process. The washing is carried out at a slower stirring speed. The purpose is as follows: to make the water fully contact while preventing emulsification.
when the separation of oil and soap is not ideal, and the oil contains more residual soap, the first washing water is diluted salt water. The stirring speed is low (about 30 r/min), and the washing water is uniformly sprayed into the oil. Standing for about 1 hour to discharge waste water, washing, draining, and recovering upper floating oil.
in the step b, the oil temperature is adjusted to 105 ℃, the vacuum degree is adjusted to 95KPa, dehydration is carried out for 60 minutes, water and air are completely removed, the dried oil is added with 3 percent of argil, after full stirring and mixing, the oil temperature is kept at 120 ℃, the oil is decolorized for about 30 minutes under the condition of residual pressure of 8KPa, and the oil is cooled to about 70 ℃ and filtered by a vibration filter through a decolorization pump.
in the step c, after the decolorization is finished, closing a steam valve, reducing the oil temperature to below 70 ℃, then filtering, stopping a decolorization oil pump when the pressure in the vibration filter reaches 3.0bar, closing an oil inlet valve, opening a cake blowing steam valve, opening a cake blowing valve when the oil outlet of an oil purifying pipeline sight glass is turbid, closing the oil purifying valve, keeping the pressure in the vibration filter at 3.0bar, blowing for 15min, opening a dirty oil outlet valve when almost no oil flows out of the cake blowing oil outlet sight glass, closing the cake blowing valve, discharging the oil stored at the bottom of the vibration filter, and after the oil is discharged completely, firstly closing a steam inlet valve and closing the dirty oil valve when a pressure gauge pointer of the vibration filter points to 0; opening a butterfly valve at the bottom of the vibrating filter, opening an air hammer valve, and when the valve is opened for a plurality of times, the vibration time is short, the time behind the valve can be long, but the vibration time cannot exceed 10s each time; and after the waste residue is discharged, closing the bottom valve in time and closing the compressed air.
In the step d, after the temperature of the oil in the deodorization pot reaches 120 ℃, directly introducing superheated steam, and rolling the crude oil, wherein the steam inlet pressure of the superheated steam cannot be too high, so that the deodorizing oil is not too much rolled; stopping heating when the oil temperature is increased to about 240 ℃, then starting heat preservation, keeping a vacuum state, continuously performing direct superheated steam deodorization for 3 hours, closing a heat conduction oil inlet and outlet valve 30 minutes before deodorization is stopped, closing a direct steam valve after deodorization, starting a deodorization oil pump, opening a deodorization pot and a cooling water inlet and outlet valve of a spiral plate heat exchanger, and pumping a finished product oil to a finished product oil tank by using the deodorization oil pump when the oil temperature is reduced to below 50 ℃.
In the step e, when the temperature of the oil product is reduced to be below 40 ℃, the temperature of the oil product is reduced to 10 ℃ according to the temperature of 3 ℃ per hour, when the temperature of the oil product is reduced to be below 10 ℃, the temperature of the oil product is reduced to be 6 ℃ according to the temperature of 0.5 ℃ per hour, the oil temperature is maintained to be about 6 ℃ finally, crystallization and crystal growth are carried out for 6 hours, then filtration is carried out, during the cooling period of the crystallization and crystal growth, the rotating speed is controlled to be 8-15 revolutions per minute, the crystallized oil is pressed into a plate and frame filter by a filter pump to be filtered, the turbid oil which is just filtered is returned to a turbid oil tank, and finally the turbid oil is returned to a crystallization tank which. After the filter layer of the filter is formed, clear oil begins to be discharged and is sent to a finished oil tank. When the filter cake of the filter reaches a certain degree and the pressure of the oil inlet pump reaches 3.0bar, then compressed air is introduced to blow the cake dry, the blown waste oil enters a turbid oil tank, and oil inlet filtration is performed again after the cake discharge is completed.
Example two
In the step a, 15 BC' concentration alkali liquor and 85% phosphoric acid are prepared in a high-level alkali liquor box, and the temperature of hot water is 95 degrees.
In the step a, the acid adding amount is controlled to be 0.05 percent of the oil amount; adding and rapidly stirring, controlling the oil temperature at 60 ℃, reacting phosphoric acid for 40 minutes, adding prepared hot water into the oil, finishing adding the hot water within 5 minutes, wherein the heating water amount is about 5 percent of the oil amount, reducing the speed to half of the original speed after adding, continuously stirring for about 20 minutes, standing for about 2-3 hours when oil residue particles are separated out, and condensing the oil residue into large particles to settle at the bottom of a water washing pot. Opening an emptying valve at the bottom of the oil refining pot, putting lower wastewater into an oil separating box, discharging the wastewater separated by the oil separating box into a wastewater pool, pumping the waste oil separated from the oil separating box into the oil refining pot by a pump for recycling, and pumping lower-layer oil residue in the oil refining pot into a soapstock pot by a gear pump after the wastewater is discharged. The two oil refining pots are circularly and alternately used according to the first-in first-out principle. Opening an alkali liquor filling valve, adding a prepared alkali liquor, calculating the alkali addition amount according to the actual acid value of the crude oil according to a formula [ theoretical alkali amount (t) ═ 7.13 multiplied by 10-4 multiplied by oil weight multiplied by acid value ], determining the excess alkali of 0.10 percent of the theoretical alkali oil weight, completing the addition of all the alkali liquor once within 5-10 minutes, simultaneously stirring rapidly (about 60 r/min), not raising the temperature immediately after the alkali addition is completed, and continuing to stir slowly for about 20-30 minutes to ensure that the alkali liquor and the acid in the oil fully react;
after the neutralization reaction is finished, the stirring speed of the oil refining kettle is slowed down (about 30 r/min), then the indirect steam is started to heat the oil, the oil is heated to 90 ℃, the heating is stopped, the heat preservation is started, the temperature is finally kept at 90 ℃ all the time, the stirring is continued for about 10min to promote the coagulation of the nigre, and the stirring is stopped when the oil and the nigre are in a separated state. The stirring speed should be reduced to about 30 rpm during the temperature rise process to prevent the soap particles from being broken up. After reaching the final temperature, the soapstock and the oil easily separate and sink quickly.
If the soapstock is sticky and in a more permanent suspension state in the production process, clear water or diluted saline water which is at the same temperature as or slightly higher than the oil temperature can be added, and the pressure water is called as pressurized water. Promoting the specific gravity of the soap particles to increase and sink after absorbing water. Adding water in an amount of 5%, stopping stirring, and standing for 3-4 hours. Opening an emptying valve at the bottom of the oil refining pot, pumping soapstock at the bottom of the oil refining pot into the soapstock pot by using a gear pump, wherein the soapstock discharge condition is observed, and the emptying valve is closed in time when oil is discharged; if necessary, carrying out secondary alkali refining, and if the soap grains are too large, increasing the neutral oil content of soapstock and not reducing the stirring speed in the temperature rising process. The washing is carried out at a slower stirring speed. The purpose is as follows: the water is sufficiently contacted while preventing emulsification.
When the separation of oil and soap is not ideal, and the oil contains more residual soap, the first washing water is diluted salt water. The stirring speed is low (about 30 r/min), and the washing water is uniformly sprayed into the oil. Standing for about 1 hour to discharge waste water, washing, draining, and recovering upper floating oil.
In the step b, the oil temperature is adjusted to 100 ℃, the vacuum degree is adjusted to 90KPa, dehydration is carried out for 60 minutes, water and air are completely removed, the dried oil is added with 3 percent of argil, after full stirring and mixing, the oil temperature is kept at 110 ℃, the oil is decolorized for about 30 minutes under the condition of residual pressure of 8KPa, and the oil is cooled to about 70 ℃ and filtered by a vibration filter through a decolorization pump.
in the step c, after the decolorization is finished, closing a steam valve, reducing the oil temperature to below 70 ℃, then filtering, stopping a decolorization oil pump when the pressure in the vibration filter reaches 3.0bar, closing an oil inlet valve, opening a cake blowing steam valve, opening a cake blowing valve when the oil outlet of an oil purifying pipeline sight glass is turbid, closing the oil purifying valve, keeping the pressure in the vibration filter at 3.0bar, blowing for 15min, opening a dirty oil outlet valve when almost no oil flows out of the cake blowing oil outlet sight glass, closing the cake blowing valve, discharging the oil stored at the bottom of the vibration filter, and after the oil is discharged completely, firstly closing a steam inlet valve and closing the dirty oil valve when a pressure gauge pointer of the vibration filter points to 0; opening a butterfly valve at the bottom of the vibrating filter, opening an air hammer valve, and when the valve is opened for a plurality of times, the vibration time is short, the time behind the valve can be long, but the vibration time cannot exceed 10s each time; and after the waste residue is discharged, closing the bottom valve in time and closing the compressed air.
In the step d, after the temperature of the oil in the deodorization pot reaches 120 ℃, directly introducing superheated steam, and rolling the crude oil, wherein the steam inlet pressure of the superheated steam cannot be too high, so that the deodorizing oil is not too much rolled; stopping heating when the oil temperature is about 230 ℃, then starting heat preservation, keeping a vacuum state, continuously performing direct superheated steam deodorization for 3 hours, closing a heat conduction oil inlet and outlet valve 30 minutes before deodorization is stopped, closing a direct steam valve after deodorization, starting a deodorization oil pump, opening a deodorization pot and a cooling water inlet and outlet valve of a spiral plate heat exchanger, and pumping a finished product oil to a finished product oil tank by using the deodorization oil pump when the oil temperature is reduced to below 50 ℃.
in the step e, when the temperature of the oil product is reduced to be below 40 ℃, the temperature of the oil product is reduced to 10 ℃ according to the temperature of 3 ℃ per hour, when the temperature of the oil product is reduced to be below 10 ℃, the temperature of the oil product is reduced to be 6 ℃ according to the temperature of 0.5 ℃ per hour, the oil temperature is maintained to be about 6 ℃ finally, crystallization and crystal growth are carried out for 6 hours, then filtration is carried out, during the cooling period of the crystallization and crystal growth, the rotating speed is controlled to be 8-15 revolutions per minute, the crystallized oil is pressed into a plate and frame filter by a filter pump to be filtered, the turbid oil which is just filtered is returned to a turbid oil tank, and finally the turbid oil is returned to a crystallization tank which. After the filter layer of the filter is formed, clear oil begins to be discharged and is sent to a finished oil tank. When the filter cake of the filter reaches a certain degree and the pressure of the oil inlet pump reaches 3.0bar, then compressed air is introduced to blow the cake dry, the blown waste oil enters a turbid oil tank, and oil inlet filtration is performed again after the cake discharge is completed.
The above description is only a preferred embodiment of the present invention, and for those skilled in the art, the present invention should not be construed as limited to the above description, but should be modified in view of the following detailed description and application range.
Claims (7)
1. A tea seed oil finish machining process is characterized in that: the method comprises the following steps:
Acidifying, neutralizing and washing, namely converting non-hydrated phospholipid into hydrated phospholipid by utilizing the reaction of phosphoric acid and non-hydrated phospholipid in the crude oil to form a hydrated phospholipid group which is easy to separate; performing neutralization reaction by using liquid alkali and free fatty acid in the crude oil to generate soap, then performing settling separation to achieve the purpose of removing phospholipid, free fatty acid and metal ions in the crude oil, and washing residual soapstock in the oil by hot water;
Drying and decoloring, removing water in the water washing oil in a vacuum state, adding white soil to mix with the oil to be decolored, and adsorbing pigment, residual nigre, phospholipid, metal ions and the like in the crude oil by using argil in the vacuum state so as to achieve the purposes of decoloring and adsorbing impurities;
Filtering, namely filtering waste argil in the oil by using a blade filter, and physically deacidifying and deodorizing the filtered decolored oil in a deodorizing pot;
Deodorizing, namely destroying the thermal-sensitive pigment in a high-temperature and high-vacuum environment, removing residual substances influencing the flavor, and simultaneously recovering fatty acid to improve the edible quality of the oil product;
Dewaxing, namely cooling the oil product, crystallizing and separating out wax with low melting point in the oil from the oil, and filtering out the wax separated out from the oil by a filtering means to obtain the finished oil.
2. The tea seed oil finishing process according to claim 1, characterized in that: in the step a, the alkali liquor with the concentration of 10BC '-16 BC' and the phosphoric acid with the concentration of 70-85% are prepared in the high-level alkali liquor tank, and the temperature of hot water is 90-100 degrees.
3. The tea seed oil finishing process according to claim 1, characterized in that: in the step a, the acid adding amount is controlled to be 0.05-0.2% of the oil amount; adding and rapidly stirring, controlling the temperature of oil at 60-65 ℃, reacting phosphoric acid for 40 minutes, adding prepared hot water into the oil, finishing adding the hot water within 5 minutes, wherein the amount of the heated water is about 5-10% of the oil amount, reducing the speed to half of the original speed after adding, continuously stirring for about 20 minutes, and standing for about 2-3 hours when oil foot particles are separated out.
4. the tea seed oil finishing process according to claim 3, characterized in that: in the step b, the oil temperature is adjusted to be 100-105 ℃, the vacuum degree is adjusted to be 85-95KPa, dehydration is carried out for 60 minutes, water and air are completely removed, the dried oil is added with 1-3% of argil, after full stirring and mixing, the oil temperature is kept at 105-120 ℃, the oil is decolorized for about 30 minutes under the condition of residual pressure of 8KPa, and the oil is cooled to about 70 ℃ and filtered out of the argil by a vibration filter through a decolorization pump.
5. The tea seed oil finishing process according to claim 1, characterized in that: and in the step c, closing the steam valve after the decolorization is finished, and cooling the oil to below 70 ℃ and then filtering.
6. the tea seed oil finishing process according to claim 1, characterized in that: in the step d, after the temperature of the oil in the deodorization pot reaches 120 ℃, directly introducing superheated steam, and rolling the crude oil, wherein the steam inlet pressure of the superheated steam cannot be too high, so that the deodorizing oil is not too much rolled; stopping heating when the oil temperature is increased to about 230-240 ℃, then starting heat preservation, keeping a vacuum state, continuously communicating direct superheated steam for deodorization for 3 hours, closing a heat conduction oil inlet and outlet valve 30 minutes before deodorization is stopped, closing a direct steam valve after deodorization, starting a deodorization oil pump, opening a deodorization pot and a cooling water inlet and outlet valve of a spiral plate heat exchanger, and pumping a finished product oil to a finished product oil tank by using the deodorization oil pump when the oil temperature is reduced to below 50 ℃.
7. The tea seed oil finishing process according to claim 1, characterized in that: in the step e, when the temperature of the oil product is reduced to be below 40 ℃, the temperature of the oil product is reduced to 10 ℃ according to the temperature reduction of 3 ℃ per hour, when the temperature of the oil product is reduced to be below 10 ℃, the temperature of the oil product is reduced to 6 ℃ according to the temperature reduction of 0.5 ℃ per hour, the oil temperature is finally kept at about 6 ℃, crystallization and crystal growth are carried out for 6 hours, then filtration is started, and during the crystallization and crystal growth cooling period, each rotating speed is required to be controlled to be 8-15 revolutions per minute.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112175728A (en) * | 2020-10-24 | 2021-01-05 | 河南华泰粮油机械股份有限公司 | Refining and sterilizing treatment method of medicinal coconut oil |
| CN114350443A (en) * | 2021-02-05 | 2022-04-15 | 广西森洲生物技术有限公司 | Separation system and process for fatty acid and oil in grease byproduct |
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| CN102504950A (en) * | 2011-11-08 | 2012-06-20 | 安徽绿健生物科技有限公司 | Method for decolorizing tea seed oil |
| CN104232292A (en) * | 2014-09-16 | 2014-12-24 | 锦屏县食为天农产品有限公司 | Cold pressing and refining method of camellia oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102504950A (en) * | 2011-11-08 | 2012-06-20 | 安徽绿健生物科技有限公司 | Method for decolorizing tea seed oil |
| CN104232292A (en) * | 2014-09-16 | 2014-12-24 | 锦屏县食为天农产品有限公司 | Cold pressing and refining method of camellia oil |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112175728A (en) * | 2020-10-24 | 2021-01-05 | 河南华泰粮油机械股份有限公司 | Refining and sterilizing treatment method of medicinal coconut oil |
| CN114350443A (en) * | 2021-02-05 | 2022-04-15 | 广西森洲生物技术有限公司 | Separation system and process for fatty acid and oil in grease byproduct |
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