CN111534374A - Method for improving content of nutritional ingredients in oil and oil refining system used for method - Google Patents
Method for improving content of nutritional ingredients in oil and oil refining system used for method Download PDFInfo
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- CN111534374A CN111534374A CN202010259152.9A CN202010259152A CN111534374A CN 111534374 A CN111534374 A CN 111534374A CN 202010259152 A CN202010259152 A CN 202010259152A CN 111534374 A CN111534374 A CN 111534374A
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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
- C11B3/12—Refining fats or fatty oils by distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/12—Molecular 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
- C11B3/001—Refining fats or fatty oils by a combination of two or more of the means hereafter
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes
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Abstract
The invention provides a method for improving the content of nutrient components in oil and a system for refining the oil, wherein the method and the system avoid the gasification and loss of the nutrient components in the distillation process by combining the pre-dehydration treatment and the one-stage or multi-stage molecular distillation treatment, effectively collect the nutrient components in the raw oil and enrich the content of the nutrient components such as vitamin E, phytosterol and the like in the refined oil.
Description
Technical Field
The invention relates to the technical field of food processing, in particular to a method for improving the content of nutrient components in oil by utilizing a molecular distillation technology and an oil refining system used for the method.
Background
The oil and fat is rich in abundant nutrients such as vitamins and phytosterol. The research finds that the phytosterol and the animal sterol cholesterol have structural similarity, are active ingredients in plants and have a plurality of important physiological functions. It is found that the total cholesterol and low density lipoprotein content in blood can be obviously reduced by supplementing phytosterol. Sierksma et al found that taking 0.8g of soy sterol per day significantly reduced the total cholesterol and low density lipoprotein levels in the blood after 3 weeks.
A particular recommended value for phytosterols in the Dietary Reference Intakes (DRIs) of the Chinese population version 2013 was 900 mg/d. The daily average intake of the phytosterol of residents in China is 322.41mg/d, which is obviously lower than a specific recommended value. According to the edible oil consumption data calculation of China, the edible oil is consumed by all people of China every day by 40 g. At present, the sterol content of common corn oil in the market is 600-800mg/100g, and the sterol content of plant required by human body cannot be effectively supplemented.
In addition, the grease contains abundant vitamin E, the vitamin E has the effects of oxidation resistance and aging resistance, and clinical experiments show that the vitamin E has obvious curative effects on diseases of the digestive system, the immune system and the like. A specific recommended value for phytosterols in the Dietary Reference Intakes (DRIs) of the Chinese residents, 2013 edition is 14 mg/d. In addition, other oils and fats such as rice oil contain nutritional components such as oryzanol, squalene, sterol, vitamin E-a tocopherol, etc.; the sunflower seed oil contains nutritional ingredients such as linoleic acid, sterol, carotene, vitamin E, vitamin B3, etc.
The boiling point of the nutrient components such as vitamin E, phytosterol and the like in the oil is low, and the nutrient components are mainly concentrated in the light-phase substances after distillation treatment. However, such nutrients are easily gasified and lost during distillation treatment, and the existing refining process is difficult to ensure that the light-phase substances are obtained in high yield in a short time and simultaneously the nutrient components can be greatly enriched in the light-phase substances.
Disclosure of Invention
In view of the above problems in the prior art, the present invention provides a method for increasing the content of nutrients in oils and fats by using molecular distillation technology, which can solve the problem of increasing the loss of nutrients in the refining process of different oils and fats.
Specifically, the invention provides a method for improving the content of the nutrient components in the oil by utilizing a molecular distillation technology, wherein the method comprises the following steps:
(1) the raw material oil is subjected to impurity removal, degumming, decoloration, alkali refining and dewaxing treatment in sequence to obtain pretreated oil;
(2) enabling the pretreated grease to enter a pre-dehydration gas system, and treating the grease by a film evaporator at the temperature of 50-100 ℃ and under the pressure of 50-150Pa to obtain grease of pre-dehydration gas; and
(3) enabling the grease of the pre-dehydrated gas to enter a primary molecular distillation system, preheating to 150-200 ℃, and then entering a first molecular distiller, wherein the distillation temperature of the first molecular distiller is 250-280 ℃, the rotation speed is 20-50 r/min, the vacuum degree is 0.1-8.0Pa, the condensation temperature is 10-35 ℃, the obtained light phase substance enters a first light phase tank after being condensed and collected, and the heavy phase substance enters a first heavy phase tank; the light phase substance is deacidified, deodorized and degreased to obtain a grease product with improved nutrient content, and the heavy phase substance is used as a byproduct.
In another aspect of the present invention there is provided a fat refining system for use in the above method of the present invention, the fat refining system comprising:
a pre-dehydration gas system comprising a first preheater, a thin film evaporator and a condenser connected in series in fluid communication;
a primary molecular distillation system which is connected with the downstream of the pre-dehydration gas system in a fluid communication manner and comprises a second preheater, a first molecular distiller and a first cold trap which are sequentially connected in a fluid communication manner, and a first heavy phase receiving tank and a first light phase receiving tank which are connected with the first molecular distiller in a fluid communication manner and are arranged in parallel;
a secondary molecular distillation system which is connected with the downstream of the primary molecular distillation system in a fluid communication manner and comprises a third preheater, a second molecular distiller and a second cold trap which are sequentially connected in a fluid communication manner, and a second heavy-phase receiving tank and a second light-phase receiving tank which are connected with the second molecular distiller in a fluid communication manner and are arranged in parallel; and
a tertiary molecular distillation system fluidly connected downstream of the secondary molecular distillation system and comprising a fourth preheater, a third molecular still and a third cold trap connected in series in fluid communication, and a third triple receiving tank and a third light phase receiving tank arranged in parallel and respectively connected to the third molecular still in fluid communication.
Advantageous effects
The method for improving the content of the nutrient components in the oil by utilizing the molecular distillation technology and the oil refining system can effectively collect the nutrient components in the raw oil in a short time (5-25 seconds) and at a high yield (40-50 percent) by combining the pre-dehydrated gas treatment and the one-stage or multi-stage molecular distillation treatment, and improve the content of the nutrient components such as vitamin E, phytosterol and the like in the refined oil; before molecular distillation, the pre-dehydrated gas treatment is carried out, so that the vacuum degree of the next-stage molecular distiller can be obviously improved, and the low pre-dehydrated gas temperature can effectively retain the nutrient components in the grease, and prevent the nutrient components from being gasified and lost.
The method and the system can improve the content of nutrient components in the grease product obtained by the primary molecular distiller by 2-3 times or even higher than that of the raw grease. For example, in the oil product obtained by the primary molecular distiller, the method can respectively increase the vitamin E (alpha-tocopherol equivalent, 20-30mg/100g) and the sterol content (6000-; the vitamin E (alpha-tocopherol equivalent, 30mg/100g) and oryzanol content (16000mg/kg) in the raw material rice oil are respectively increased to 40mg-60mg/100g and 25000-28000 mg/kg.
Drawings
FIG. 1 is a schematic perspective view of a fat refining system of the present invention that can be used in the method of the present invention for increasing the nutrient content of fat using molecular distillation;
the parts in the drawings are numbered as follows: 1-1 a first preheater; 1-2 second preheater; 1-3 third preheater; 1-4 fourth preheater; 2, a thin film evaporator; 3 a first molecular still; 4 a second molecular still; 5 a third molecular still; 6, a condenser; 7-1 a first cold trap; 7-2 second cold trap; 7-3, a third cold trap; 8-1 a first receiving tank; 8-2 a second receiving tank; 8-3 a first heavy phase receiver tank; 8-5 second double-phase receiving tank; 8-7, a third layer receiving tank; 8-4 a first light phase receiving tank; 8-6 second light phase receiving tank; 8-8 of a third light phase receiving tank; 9-1 a first vacuum unit; 9-2 a second vacuum unit; 9-3, a third vacuum unit; 9-4 fourth vacuum machine set.
Detailed Description
The following describes in detail specific embodiments of the present invention. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
In the present invention, unless otherwise specified, the term "oil" refers to an edible oil selected from the group consisting of corn oil, sunflower oil, peanut oil, rapeseed oil, rice bran oil, tea tree seed oil, and processed products and mixtures thereof. In the present invention, the rice oil is a processed product of rice bran oil.
In the present invention, unless otherwise specified, the term "nutrient" is selected from vitamin E (alpha tocopherol), polypeptides, sterols, squalene, oryzanol, linoleic acid, carotene, vitamin B3 and polypeptides. The method and the system can enrich the characteristic nutrient components aiming at different raw material grease. Illustratively, the method and system of the present invention can enrich oryzanol, squalene, sterol, vitamin E-a tocopherol, etc. contained in rice oil; sterols contained in corn oil, etc.; linoleic acid, sterol, carotene, vitamin E, vitamin B3, etc. in sunflower seed oil.
In the present invention, unless otherwise specified, the term "increase in the content of nutrients" or "increase in the content of nutrients" means that the content of nutrients in the oil or fat product is increased by 2 to 3 times or even more relative to the starting oil or fat.
In the present invention, "light phase receiving tank" and "light phase tank" may be used interchangeably; the "heavy phase receiving tank" and "heavy phase tank" may be used interchangeably.
In one embodiment, the invention provides a method for improving the content of the nutrient components in the grease by using a molecular distillation technology, wherein the method comprises the following steps:
(1) the raw material oil is subjected to impurity removal, degumming, decoloration, alkali refining and dewaxing treatment in sequence to obtain pretreated oil;
(2) enabling the pretreated grease to enter a pre-dehydration gas system, and treating the grease by a film evaporator at the temperature of 50-100 ℃ and under the pressure of 50-150Pa to obtain grease of pre-dehydration gas; and
(3) enabling the grease of the pre-dehydrated gas to enter a primary molecular distillation system, preheating to 150-200 ℃, and then entering a first molecular distiller, wherein the distillation temperature of the first molecular distiller is 250-280 ℃, the rotation speed is 20-50 r/min, the vacuum degree is 0.1-8.0Pa, the condensation temperature is 10-35 ℃, the obtained light phase substance enters a first light phase tank after being condensed and collected, and the heavy phase substance enters a first heavy phase tank; the light phase substance is deacidified, deodorized and degreased to obtain a grease product with improved nutrient content, and the heavy phase substance is used as a byproduct.
In the present invention, the removal of impurities, degumming, decoloring, caustic refining and dewaxing in step (1) is not particularly limited as long as impurities, pigments and the like in the raw oil and fat can be removed, and any conventional treatment method in the art can be used.
In a preferred embodiment, in the step (1), the raw oil is selected from the group consisting of corn oil, sunflower oil, peanut oil, rapeseed oil, rice oil, tea tree seed oil, and a mixture thereof.
In a preferred embodiment, the method for increasing the content of the nutritional components in the fat or oil by using the molecular distillation technology of the present invention comprises the steps (1) to (3) described above.
In a preferred embodiment, the step (2) further satisfies one or more of the following conditions:
the feeding amount of the pretreated grease is 10-30 tons;
the feeding flow rate of the pretreated grease is 900L/h-1500L/h;
the treatment temperature of the pre-dehydrated water vapor is 60-70 ℃; and
the vacuum degree of the pre-dehydrated water vapor is 55-70 Pa.
The inventor finds that because the boiling point of nutrient components such as vitamin E, phytosterol and the like in the grease is low, nutrient components in the grease can be enriched and retained in the grease with pre-dehydrated water to the maximum extent by enabling the pretreated grease to enter a film evaporator in the step (2), controlling the temperature of pre-dehydrated gas to be 50-100 ℃ (preferably 60-70 ℃), and controlling the vacuum degree of the pre-dehydrated gas to be 50-150Pa (preferably 55-70 Pa). Furthermore, the removal of light substances such as water vapor and the like in the raw oil can obviously improve the vacuum degree of the subsequent molecular distillation treatment, is beneficial to maximally enriching nutrient substances in a short time, and maximally reduces the further gasification and loss of the nutrient substances.
In one embodiment, the step (3) further satisfies one or more of the following conditions:
the preheating temperature is 170-180 ℃;
the distillation temperature of the first molecular distiller is 275-280 ℃;
the rotating speed of the first molecular distiller is 30-38 r/min;
the vacuum degree of the first molecular distiller is 0.1-0.3 Pa;
the condensation temperature of the first molecular distiller is 20-30 ℃; and
the distillation time of the evaporation surface of the first molecular still is 5-25 seconds.
In the step (3), the vacuum degree of the primary molecular distillation treatment is obviously improved because light substances such as water vapor and the like in the raw material grease are removed in the step (2). The oil and fat which is pre-dehydrated in the first molecular distillation apparatus is treated under the improved vacuum degree (0.1-8.0Pa) and the increased temperature (250-280 ℃), so that the light-phase component can be obtained in a short time (5-25 seconds) with a desired yield, simultaneously, nutrient substances are maximally enriched in the light-phase component in a short time, and the gasification and the loss of the nutrient substances in the molecular distillation treatment are further avoided.
In one embodiment, the method for increasing the content of the nutritional ingredients in the oil and fat by using the molecular distillation technology further comprises the following step (4):
(4) enabling the heavy phase substance obtained in the step (3) to further enter a secondary molecular distillation system, wherein the heavy phase substance enters a second molecular distiller after being preheated to 250 ℃, the distillation temperature of the second molecular distiller is 281-300 ℃, the rotation speed is 20-50 r/min, the vacuum degree is 0.1-8.0Pa, the condensation temperature is 10-35 ℃, the obtained light phase substance enters a second light phase tank after being condensed and collected, and the heavy phase substance enters a second heavy phase tank as a byproduct; and (4) mixing the light-phase substance obtained in the step (4) with the light-phase substance obtained in the step (3), and performing deacidification, deodorization and degreasing to obtain the grease product with the content of the nutrient components improved.
In a preferred embodiment, the step (4) further satisfies one or more of the following conditions:
the preheating temperature is 220-240 ℃;
the distillation temperature of the second molecular distiller is 295-300 ℃;
the rotating speed of the second molecular distiller is 35-45 r/min;
the vacuum degree of the second molecular distiller is 0.1-0.2 Pa; and
the condensation temperature of the second molecular distiller is 20-30 ℃.
In the step (4), the condensed water has a temperature of 10 to 35 deg.C (preferably 20 to 30 deg.C), enabling the light-phase component molecules to be completely condensed and trapped to the maximum extent.
In the present invention, the deacidification, deodorization and degreasing in the steps (3) and (4) are not particularly limited as long as impurities such as odor in the product can be removed, and any conventional treatment method in the art can be adopted.
In one embodiment, the method for improving the content of the nutritional ingredients in the oil and fat by using the molecular distillation technology further comprises the following step (5):
(5) and (3) further feeding the heavy phase substance obtained in the step (4) into a three-stage molecular distillation system, wherein the heavy phase substance enters a third molecular distiller after being preheated to the temperature of 250-.
In a preferred embodiment, said step (5) further satisfies one or more of the following conditions:
the preheating temperature is 250-270 ℃;
the distillation temperature of the third molecular distiller is 315-320 ℃;
the rotating speed of the third molecular distiller is 40-45 r/min;
the vacuum degree of the third molecular distiller is 0.1-0.2 Pa; and
the condensation temperature of the third molecular still is 20-30 ℃.
In the step (5), the distillation temperature of the third molecular still is 301-.
In the invention, the rotating speed of the molecular distiller is specially controlled to be 20-50 rpm, so that the grease can be uniformly formed into a film in the molecular distiller. In the present invention, the distillation time in step (4) and step (5) is not particularly limited, and those skilled in the art can flexibly adjust the distillation time according to the required amount of the product.
In another embodiment, the present invention provides a fat refining system for use in the above method of the present invention, the fat refining system comprising:
a pre-dehydration gas system comprising a first preheater, a thin film evaporator and a condenser connected in series in fluid communication;
a primary molecular distillation system which is connected with the downstream of the pre-dehydration gas system in a fluid communication manner and comprises a second preheater, a first molecular distiller and a first cold trap which are sequentially connected in a fluid communication manner, and a first heavy phase receiving tank and a first light phase receiving tank which are connected with the first molecular distiller in a fluid communication manner and are arranged in parallel;
a secondary molecular distillation system which is connected with the downstream of the primary molecular distillation system in a fluid communication manner and comprises a third preheater, a second molecular distiller and a second cold trap which are sequentially connected in a fluid communication manner, and a second heavy-phase receiving tank and a second light-phase receiving tank which are connected with the second molecular distiller in a fluid communication manner and are arranged in parallel; and
a tertiary molecular distillation system fluidly connected downstream of the secondary molecular distillation system and comprising a fourth preheater, a third molecular still and a third cold trap connected in series in fluid communication, and a third triple receiving tank and a third light phase receiving tank arranged in parallel and respectively connected to the third molecular still in fluid communication.
In a preferred embodiment, the pre-dehydrated gas system further comprises a first receiving tank and a second receiving tank disposed in parallel in fluid communication downstream of the thin film evaporator and the condenser.
In a preferred embodiment, a first vacuum unit, a second vacuum unit, a third vacuum unit and a fourth vacuum unit are respectively arranged after the pre-dehydration gas system, the primary molecular distillation system, the secondary molecular distillation system and the tertiary molecular distillation system.
The method for improving the content of the nutrient components in the oil by utilizing the molecular distillation technology and the oil refining system combine physical refining methods such as pre-dehydrated gas treatment and one-stage or multi-stage molecular distillation treatment, strictly and accurately control parameters such as temperature, vacuum degree, rotating speed, cooling water temperature and the like in the treatment process, can effectively enrich a large amount of nutrient components in the oil (the nutrient components enriched in the first molecular distiller are the most) in the distillation process of the first molecular distiller or the second molecular distiller, and cannot damage the oil structure.
Examples
For a better understanding of the present invention, the present invention is further described below with reference to the accompanying drawings and examples, which are not intended to limit the scope of the present invention. The experimental methods described in the examples are all conventional methods unless otherwise specified; such raw materials as corn oil, unless otherwise specified, are commercially available or may be synthesized using or according to methods known in the art. Corn oil (corn oil) and rice bran oil used in the examples were purchased from conventional commercial sources.
Example 1
This example provides a method for improving the nutritional content of corn oil using molecular distillation techniques.
1. The raw material corn oil is subjected to impurity removal, degumming, decoloration, alkali refining and dewaxing treatment to obtain the pretreated corn oil.
2. Enabling the pretreated corn oil obtained in the step 1 to enter a pre-dehydration gas system, and treating and removing water vapor in the oil through a film evaporator 2 to obtain the corn oil of pre-dehydration gas; wherein the feeding amount of the pretreated corn oil is 15 tons each time, the feeding flow is 900L/h, the pre-dehydration and degassing temperature is 60 +/-1 ℃, and the pre-dehydration and degassing vacuum degree is 60 Pa.
3. Preheating the pre-dewatered corn oil in the step 2, then feeding the preheated corn oil into a first molecular distiller 3 in a primary molecular distillation system for distillation, wherein the temperature of a preheater 1-2 is 170 ℃, the distillation temperature of the first molecular distiller 3 is 280 +/-1 ℃, the vacuum degree is 0.3Pa, the scraper rotating speed of the first molecular distiller 3 is 30r/min, the temperature of condensed water is 20 ℃, the distillation time of an evaporation surface is 5-25 seconds, and the obtained light-phase substance is condensed and collected and then enters a light-phase receiving tank 8-4. Detection shows that the content of vitamin E (alpha-tocopherol equivalent) in the light phase substance is as high as 100.5mg/100 g; the phytosterol content is up to 24210.7 mg/kg. The light phase material was calculated to be about 51.2% of the feed. The heavy phase material enters a heavy phase receiving tank 8-3 of the stage, and the next stage is distilled for standby.
4. And (3) allowing the heavy phase substances in the heavy phase tank 8-3 in the step (3) to enter a second molecular distiller 4 in a secondary molecular distillation system for distillation, wherein the temperature of a preheater 1-3 is 220 ℃, the distillation temperature of the second molecular distiller 4 is 300 +/-1 ℃, the vacuum degree is 0.2Pa, the scraper rotating speed of the second molecular distiller 4 is 35r/min, the temperature of condensed water is 20 ℃, and collecting the light phase substances to enter a light phase receiving tank 8-6, wherein the content of vitamin E (alpha-tocopherol equivalent) in the light phase substances is 0.8mg/100g, and the content of phytosterol is 6776 mg/kg. The heavy phase material enters a heavy phase receiving tank 8-5 for three-stage molecular distillation for standby.
5. And (3) allowing the heavy phase substances in the heavy phase tanks 8-5 in the step (4) to enter a third molecular distiller 5 in a three-stage molecular distillation system for distillation, wherein the temperature of a preheater 1-4 is 260 ℃, the distillation temperature of the third molecular distiller 5 is 315 +/-1 ℃, the vacuum degree is 0.1Pa, the scraper rotating speed of the third molecular distiller 5 is 40r/min, the temperature of condensed water is 20 ℃, and collecting light phase substances to enter a light phase receiving tank 8-8, wherein the content of vitamin E (alpha-tocopherol equivalent) in the light phase substances is 2.3mg/100g, the content of phytosterol is 3628.3mg/kg, and the light phase substances are taken as byproducts for sale. The heavy phase material enters the heavy phase receiver tank 8-7 for sale as a by-product.
6. And (4) mixing the light-phase substances obtained in the step (3) and the step (4) to obtain the mixed corn oil, wherein the content of vitamin E (alpha-tocopherol equivalent) is up to 47.78mg/100g, and the content of phytosterol is up to 11509.77 mg/kg.
Example 2
This example provides a method for improving the nutritional content of corn oil using molecular distillation techniques.
1. The raw material corn oil is subjected to impurity removal, degumming, decoloration, alkali refining and dewaxing treatment to obtain the pretreated corn oil.
2. The pre-treated corn oil obtained in the step 1 enters a pre-dehydration gas system, and is treated by a film evaporator 2 to remove water vapor in the oil, so that the corn oil of the pre-dehydration gas is obtained; wherein the feeding amount of the pretreated corn oil is 30 tons each time, the feeding flow is 1500L/h, the temperature of the pre-dehydration and degassing is 70 +/-1 ℃, and the vacuum degree of the pre-dehydration and degassing is 55 Pa.
3. Preheating the pre-dewatered corn oil in the step 2, then feeding the preheated corn oil into a first molecular distiller 3 in a primary molecular distillation system for distillation, wherein the temperature of a preheater 1-2 is 180 ℃, the distillation temperature of the first molecular distiller 3 is 278 +/-1 ℃, the vacuum degree is 0.2Pa, the scraper rotating speed of the first molecular distiller 3 is 35r/min, the temperature of condensed water is 25 ℃, the distillation time of an evaporation surface is 5-25 seconds, and the obtained light-phase substance is condensed and collected and then enters a light-phase receiving tank 8-4. Detection shows that the content of vitamin E (alpha-tocopherol equivalent) in the light phase substance is up to 68.6mg/100 g; the phytosterol content is up to 19617.4 mg/kg. The light phase material was calculated to be about 49.5% of the feed. The heavy phase material enters a heavy phase receiving tank 8-3 of the stage, and the next stage is distilled for standby.
4. And (3) allowing the heavy phase substances in the heavy phase tank 8-3 in the step (3) to enter a second molecular distiller 4 in a secondary molecular distillation system for distillation, wherein the temperature of a preheater 1-3 is 220 ℃, the distillation temperature of the second molecular distiller 4 is 295 +/-1 ℃, the vacuum degree is 0.2Pa, the scraper rotating speed of the second molecular distiller 4 is 40r/min, the temperature of condensed water is 25 ℃, and collecting the light phase substances to enter a light phase receiving tank 8-6, wherein the content of vitamin E (alpha-tocopherol equivalent) in the light phase substances is 0.6mg/100g, and the content of phytosterol is 5055.3 mg/kg. The heavy phase material enters a heavy phase receiving tank 8-5 for three-stage molecular distillation for standby.
5. And (3) allowing the heavy-phase substances in the heavy-phase tank 8-5 in the step (4) to enter a third molecular distiller 5 in a three-stage molecular distillation system for distillation, wherein the temperature of a preheater 1-4 is 270 ℃, the temperature of the third molecular distiller 5 is 315 +/-1 ℃, the vacuum degree is 0.2Pa, the scraper rotating speed of the third molecular distiller 5 is 45r/min, the temperature of condensed water is 25 ℃, and collecting the light-phase substances to enter a light-phase receiving tank 8-8, wherein the content of vitamin E (alpha-tocopherol equivalent) in the light-phase substances is 0.6mg/100g, the content of phytosterol is 1416.7mg/kg, and the light-phase substances are taken as byproducts for sale. The heavy phase material enters the heavy phase receiver tank 8-7 for sale as a by-product.
6. And (4) mixing the light-phase substances obtained in the steps (3) and (4) to obtain the mixed corn oil, wherein the content of vitamin E (alpha-tocopherol equivalent) is up to 37.47mg/100g, and the content of phytosterol is up to 12188.25 mg/kg.
Example 3
This example provides a method for improving the nutritional content of rice bran oil using molecular distillation.
1. The raw material rice bran oil is subjected to impurity removal, degumming, decoloration, alkali refining and dewaxing treatment to obtain the pretreated rice bran oil (namely the rice oil).
2. The rice bran oil obtained in the step 1 enters a pre-dehydration gas system, and is treated by a film evaporator 2 to remove water vapor in grease, so that rice bran oil with pre-dehydrated water vapor is obtained; wherein the feeding amount of the pretreated rice bran oil is 10 tons each time, the feeding flow rate is 900L/h, the pre-dehydration and degassing temperature is 70 +/-1 ℃, and the vacuum degree of the pre-dehydration gas is 70 Pa.
3. Preheating the rice bran oil of the pre-dehydrated gas in the step 2, then, feeding the preheated rice bran oil into a first molecular distiller 3 in a primary molecular distillation system for distillation, wherein the temperature of a preheater 1-2 is 180 ℃, the distillation temperature of the first molecular distiller 3 is 275 +/-1 ℃, the vacuum degree is 0.1Pa, the scraper rotating speed of the first molecular distiller 3 is 38r/min, the temperature of condensed water is 30 ℃, the distillation time of an evaporation surface is 5-25 seconds, and collecting light-phase substances to enter a light-phase receiving tank 8-4. Through detection, the content of vitamin E (alpha-tocopherol equivalent) in the light phase substance is up to 50.99mg/100 g; the phytosterol content is as high as 24410mg/kg, and the oryzanol content is as high as 26560 mg/kg. The light phase material was calculated to be about 52.5% of the feed. The heavy phase material enters a heavy phase receiving tank 8-3 of the stage, and the next stage is distilled for standby.
4. And (3) allowing the heavy-phase substance in the heavy-phase tank 8-3 in the step (3) to enter a second molecular distiller 4 in a secondary molecular distillation system for distillation, wherein the temperature of a preheater 1-3 is 240 ℃, the distillation temperature of the second molecular distiller 4 is 298 +/-1 ℃, the vacuum degree is 0.1Pa, the scraper rotating speed of the second molecular distiller 4 is 43r/min, the temperature of condensed water is 30 ℃, and collecting the light-phase substance to enter a light-phase receiving tank 8-6, wherein the content of vitamin E (alpha-tocopherol equivalent) in the light-phase substance reaches 8.95mg/100g, the content of phytosterol reaches 7832mg/kg, and the content of oryzanol reaches 16576 mg/kg. The heavy phase material enters a heavy phase receiving tank 8-5 for three-stage molecular distillation for standby.
5. And (3) distilling the heavy substances in the heavy phase tanks 8-5 in the step (4) by a third molecular distiller 5 in a three-stage molecular distillation system, wherein the temperature of a preheater 1-4 is 250 ℃, the temperature of the third molecular distiller 5 is 316 +/-1 ℃, the vacuum degree is 0.2Pa, the scraper rotating speed of the third molecular distiller 5 is 45r/min, the temperature of condensed water is 30 ℃, and collecting the light phase substances into a light phase receiving tank 8-8, wherein the content of vitamin E (alpha-tocopherol equivalent) in the light phase substances is 4.55mg/100g, the content of phytosterol is 2595mg/kg, the content of oryzanol reaches 7500mg/kg, and the light phase substances are sold as byproducts. The heavy phase material enters the heavy phase receiver tank 8-7 for sale as a by-product.
6. And (4) mixing the light-phase substances obtained in the steps (3) and (4) to obtain the mixed rice bran oil, wherein the content of vitamin E (alpha-tocopherol equivalent) is up to 31.18mg/100g, the content of phytosterol is up to 16166.7mg/kg, and the content of oryzanol is 20409.6 mg/kg.
Comparative example
The present inventors studied the effect of using different evaporators in step (2) or step (3) on the enrichment of nutrients in fats and oils by comparative example 1 and comparative example 2.
TABLE 1
The foregoing is a more detailed description of the invention in connection with specific preferred embodiments and it is not intended that the invention be limited to these specific details. For those skilled in the art to which the invention pertains, several simple deductions or substitutions can be made without departing from the spirit of the invention, and all shall be considered as belonging to the protection scope of the invention.
Claims (10)
1. A method for improving the content of nutritional ingredients in oil by utilizing a molecular distillation technology comprises the following steps:
(1) the raw material oil is subjected to impurity removal, degumming, decoloration, alkali refining and dewaxing treatment in sequence to obtain pretreated oil;
(2) enabling the pretreated grease to enter a pre-dehydration gas system, and treating the grease by a film evaporator at the temperature of 50-100 ℃ and under the pressure of 50-150Pa to obtain grease of pre-dehydration gas; and
(3) the grease of the pre-dehydrated gas enters a primary molecular distillation system, enters a first molecular distiller after being preheated to 150-200 ℃, the distillation temperature of the first molecular distiller is 250-280 ℃, the rotating speed is 20-50 r/min, the vacuum degree is 0.1-8.0Pa, the condensation temperature is 10-35 ℃, the obtained light phase substance enters a first light phase tank after being condensed and collected, and the heavy phase substance enters a first heavy phase tank; the light phase substance is deacidified, deodorized and degreased to obtain a grease product with improved nutrient content, and the heavy phase substance is used as a byproduct.
2. The method according to claim 1, wherein in the step (1), the raw oil is selected from the group consisting of corn oil, sunflower oil, peanut oil, rapeseed oil, rice oil, tea tree seed oil, and a mixture thereof;
preferably, the nutritional ingredients include, but are not limited to: vitamin E, polypeptide, sterol, squalene, oryzanol, linoleic acid, carotene, vitamin B3 and polypeptide.
3. The method of claim 1 or 2, wherein the step (2) further satisfies one or more of the following conditions:
the feeding amount of the pretreated grease is 10-30 tons;
the feeding flow rate of the pretreated grease is 900L/h-1500L/h;
the treatment temperature of the pre-dehydrated water vapor is 60-70 ℃; and
the vacuum degree of the pre-dehydrated water vapor is 55-70 Pa.
4. The method of any one of claims 1-3, wherein the step (3) further satisfies one or more of the following conditions:
the preheating temperature is 170-180 ℃;
the distillation temperature of the first molecular distiller is 275-280 ℃;
the rotating speed of the first molecular distiller is 30-38 r/min;
the vacuum degree of the first molecular distiller is 0.1-0.3 Pa;
the condensation temperature of the first molecular distiller is 20-30 ℃; and
the distillation time of the evaporation surface of the first molecular still is 5-25 seconds.
5. The method according to any one of claims 1-4, wherein the method further comprises the step (4) of:
step (4) enabling the heavy phase substance obtained in the step (3) to further enter a secondary molecular distillation system, and entering a second molecular distiller after preheating to 250 ℃ of 200-; and (4) mixing the light-phase substance obtained in the step (4) with the light-phase substance obtained in the step (3), and performing deacidification, deodorization and degreasing to obtain the grease product with the content of the nutrient components improved.
6. The method of claim 5, wherein the step (4) further satisfies one or more of the following conditions:
the preheating temperature is 220-240 ℃;
the distillation temperature of the second molecular distiller is 295-300 ℃;
the rotating speed of the second molecular distiller is 35-45 r/min;
the vacuum degree of the second molecular distiller is 0.1-0.2 Pa; and
the condensation temperature of the second molecular distiller is 20-30 ℃.
7. The method according to claim 5 or 6, wherein the method further comprises the step (5) of:
and (5) enabling the heavy phase substance obtained in the step (4) to further enter a three-stage molecular distillation system, preheating to the temperature of 250-.
8. The method of claim 7, wherein the step (5) further satisfies one or more of the following conditions:
the preheating temperature is 250-270 ℃;
the distillation temperature of the third molecular distiller is 315-320 ℃;
the rotating speed of the third molecular distiller is 40-45 r/min;
the vacuum degree of the third molecular distiller is 0.1-0.2 Pa; and
the condensation temperature of the third molecular still is 20-30 ℃.
9. A grease refining system for use in the method defined in any one of claims 1-8, the grease refining system comprising:
a pre-dehydration gas system comprising a first preheater, a thin film evaporator and a condenser connected in series in fluid communication;
a primary molecular distillation system which is connected with the downstream of the pre-dehydration gas system in a fluid communication manner and comprises a second preheater, a first molecular distiller and a first cold trap which are sequentially connected in a fluid communication manner, and a first heavy phase receiving tank and a first light phase receiving tank which are connected with the first molecular distiller in a fluid communication manner and are arranged in parallel;
a secondary molecular distillation system which is connected with the downstream of the primary molecular distillation system in a fluid communication manner and comprises a third preheater, a second molecular distiller and a second cold trap which are sequentially connected in a fluid communication manner, and a second heavy-phase receiving tank and a second light-phase receiving tank which are connected with the second molecular distiller in a fluid communication manner and are arranged in parallel; and
a tertiary molecular distillation system fluidly connected downstream of the secondary molecular distillation system and comprising a fourth preheater, a third molecular still and a third cold trap connected in series in fluid communication, and a third triple receiving tank and a third light phase receiving tank arranged in parallel and respectively connected to the third molecular still in fluid communication.
10. The grease refining system as recited in claim 9 wherein the pre-dewatering gas system further comprises a first receiving tank and a second receiving tank disposed in parallel in fluid communication downstream of the thin film evaporator and the condenser; preferably, a first vacuum unit, a second vacuum unit, a third vacuum unit and a fourth vacuum unit are respectively arranged behind the pre-dehydration gas system, the primary molecular distillation system, the secondary molecular distillation system and the tertiary molecular distillation system.
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| CN112126515A (en) * | 2020-09-23 | 2020-12-25 | 周红茹 | Oil refining method |
| CN112126514A (en) * | 2020-09-23 | 2020-12-25 | 周红茹 | Oil and fat refining system |
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| CN104611130A (en) * | 2015-01-20 | 2015-05-13 | 南阳魏健稻谷油脂有限公司 | Preparation process of nutritional rice oil rich in oryzanol and vitamin E |
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| CN205953958U (en) * | 2016-07-19 | 2017-02-15 | 广州市海珥玛植物油脂有限公司 | Oil treatment system of one -level film second grade molecular distillation device |
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| CN102210352A (en) * | 2011-04-12 | 2011-10-12 | 山东三星玉米产业科技有限公司 | Vitamin AE maize oil and preparation method thereof |
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| CN112126514A (en) * | 2020-09-23 | 2020-12-25 | 周红茹 | Oil and fat refining system |
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