CN110982619A - Process capable of effectively improving content of linolenic acid in refined vegetable oil - Google Patents
Process capable of effectively improving content of linolenic acid in refined vegetable oil Download PDFInfo
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- CN110982619A CN110982619A CN201911122466.8A CN201911122466A CN110982619A CN 110982619 A CN110982619 A CN 110982619A CN 201911122466 A CN201911122466 A CN 201911122466A CN 110982619 A CN110982619 A CN 110982619A
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- oil
- tower
- deodorization
- linolenic acid
- deodorization tower
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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
-
- 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
- C11B3/14—Refining fats or fatty oils by distillation with the use of indifferent gases or vapours, e.g. steam
Abstract
The invention discloses a process capable of effectively improving the content of linolenic acid in refined vegetable oil, wherein a deodorization tower and a physical deacidification tower adopt lower control temperature, oil does not stay on a tray in the middle of the deodorization tower, so that the evaporation area and the stay volume of the deodorization tower are reduced by one third, the treatment capacity is increased, the stay time is less than 40 minutes, the deodorization tower is arranged as a double-layer tray, the temperature of the deacidification tower is reduced by 30-31 ℃ and is controlled at 209 ℃ in addition to 208 ℃, the temperature of heat transfer oil is controlled at 218 ℃ in addition to 216 ℃, the stay time of the oil in the deodorization tower is shortened to about 35-38 minutes, the vacuum degree is-0.097-0.099 MPa, and the feeding flow of the deodorization tower is improved to 3.1-3.2 tons/hour; the invention has the advantages that: obviously reduces the consumption of clay and charcoal, has high oil production efficiency, short production period and low oil loss, obviously increases the linolenic acid content by 6 to 10 percent, and obviously reduces the trans-fatty acid which is unfavorable for health.
Description
Technical Field
The invention relates to a deodorization process for vegetable oil rich in linolenic acid, in particular to a process capable of effectively improving the content of linolenic acid in refined vegetable oil, and belongs to the field of vegetable oil deodorization processes.
Background
The edible vegetable oil contains essential fatty acid which cannot be synthesized by human body, but is also important in the nutritional variety of people, and particularly has further requirements on functional and nutritional edible oil, the polyunsaturated fatty acid which cannot be synthesized by human body itself or is synthesized in a small amount in human body is difficult to meet the physiological needs, the polyunsaturated fatty acid which must be taken from food is called Essential Fatty Acid (EFA), the naturally occurring essential fatty acid is linoleic acid, linolenic acid and arachidonic acid, the linolenic acid is the polyunsaturated fatty acid with three double bonds, the linolenic acid is generally called α linolenic acid, the linolenic acid is a core substance for maintaining the brain evolution of human, the final metabolite and DHA of the substance form the important components of nerve cells, α a linolenic acid has the physiological functions of enhancing intelligence, improving memory, regulating blood pressure, preventing myocardial infarction and cerebral embolism, reducing blood fat, inhibiting complications of diabetes and the like, the essential fatty acid exists in the vegetable oil, the EPA cannot be synthesized by human body itself, but the high linolenic acid content is rich in the deodorized intelligence, the oil, the control of myocardial infarction and the trans-linolenic acid content is not influenced by the traditional deodorizing technology for a large-scale deodorizing technology, the high linolenic acid content of the trans-producing the oil is not disclosed, but the technology is not required for maintaining the trans-refining technology for a long-refining process under the condition of the high-refining technology of the trans-producing the trans-oil at the condition of the trans-producing high-producing of the trans-producing oil at the trans-producing of the trans-producing oil, which is not disclosed in the trans-enriched vegetable oil at the trans-enriched nutrient oil at the temperature of the year 35.
At present, the traditional refining of crude oil into first-grade oil needs four sections: 1 hydration degumming working section, 2 decoloring working section, 3 dewaxing working section, 4 deodorization working section → first-level finished oil;
each section removes impurities with different properties and types and different undesirable components in the vegetable oil; wherein, the specific operation of the decoloring working section is as follows: the method comprises the following steps of heating hydrated degummed crude oil (or crude oil without gum in raw materials) to 90-115 ℃ by a steam heater → a premixer → a decoloring tower (oil mixed with an adsorbent at the bottom of the tower is pumped to the bottom of the tower) → a leaf filter → a decolorized clear oil tank → a 3 dewaxing section; the concrete operation of the deodorization workshop section is as follows: dewaxing working section → dewaxed oil enters a gas separator for distillation after being heated by a heat exchanger, and then is pumped into an oil-oil heat exchanger and a (heat conducting oil) heater, after the temperature is continuously raised, the temperature is raised to 228-. After the first-grade oil produced by the traditional process method is adopted, the linolenic acid content is only 43-47% and is almost lost by 10% (the linolenic acid content of raw material crude oil is generally 53-57%), and the trans-fatty acid content is about 1.1% and is higher.
Disclosure of Invention
In order to solve the problems, the invention designs a process capable of effectively improving the linolenic acid content in refined vegetable oil, a deodorization tower and a physical deacidification tower adopt lower control temperature, oil does not stay on a tray in the middle of the deodorization tower, so that the deodorization tower reduces one third of evaporation area and retention volume, the treatment capacity is increased, the retention time is less than 40 minutes, the linolenic acid content of the linseed oil after refining is effectively improved, and the beneficial unsaturated fatty acid in a common control scheme is prevented from being converted into harmful trans-fatty acid (TFA).
The technical scheme of the invention is as follows:
a process for effectively increasing the content of linolenic acid in refined vegetable oil comprises a decoloring section and a deodorizing section;
the specific operation of the decoloring section is as follows: heating the crude oil degummed by hydration or the crude oil without glue in the raw material to 100-120 ℃ by a steam heater to reach the temperature point of good clay activity and strong adsorption capacity, and reducing the stripping load of a rear-section deodorization working section by improving the refining depth; then adding argil and active carbon into filter aid pearlite according to a certain proportion to form new adsorbent, stirring and mixing crude oil and adsorbent by means of premixer, adopting the combined adsorbent whose bulk density is moderate after mixing, because the granules are different in size, the surface of larger pearlite granule is uneven and mutually extruded, and their surface is serrated, and they can be mutually engaged and connected to form coarse filter gap, at the same time of forming filter cake on the filter plate it can provide a relatively uniform and loose support structure for other smaller two kinds of adsorbent granules so as to raise the void ratio of filter cake formed finally, and can maximally utilize adsorption capacity of argil and active carbon while retaining higher continuous permeability, so that the switching period of filter can be prolonged, and the dosage of white clay adsorbent can be greatly reduced, so that at the same time of ensuring decolouring capacity, the consumption of the clay is reduced, and the oil product is prevented from being infected with the clay taste in the decoloring process section; then distilling some non-ideal volatile light components in a decoloring tower with vacuumizing and steam to extract the light components from the top of the tower, pumping oil mixed with an adsorbent at the bottom of the tower to a filter through a pump at the bottom of the tower, wherein the filter is switched for use by two sets, and clear oil filtered by the filter enters a decoloring clear oil tank, temporarily stores the decolored clear oil, and then enters the next working section, namely a dewaxing working section;
the concrete operation of the deodorization workshop section is as follows: the dewaxed oil is heated by a heat exchanger, enters a gas separator for negative pressure distillation, is pumped into an oil-oil heat exchanger and a heater, is heated continuously to 190-200 ℃ in a deodorization tower with the vacuum degree of not less than-0.096 Mpa, so that the original oil product is reduced to only pass through an upper layer and a lower layer by three layers of tower trays in the deodorization tower, the retention time of the oil product in high temperature is reduced, the retention time after the tower trays is reduced is 40 minutes, and meanwhile, the treatment capacity is improved to 3.1-3.2 tons/hour for ensuring that the retention time is less than 40 minutes; the bottom of the deodorization tower is pumped into a physical deacidification tower, the liquid level of the deacidification tower is controlled to be 0.06 m at the lowest limit, the retention time of oil products at high temperature is further reduced, the temperature is controlled to be 209-215 ℃, steam distillation is carried out under high vacuum, free fatty acid and low molecular substances are discharged into a fatty acid catcher along with steam, and the bottom of the tower is pumped into a polishing filter to be subjected to heat exchange and cooling through an oil-oil heat exchanger and cooling through a finished oil cooler, so that the first-stage oil is finally obtained and sent into a finished oil tank.
Wherein the clay has a bulk density of: 0.70g/mL, bulk density of the perlite: 0.18g/mL, bulk density of the activated carbon: 0.31 g/mL.
The perlite, the argil and the activated carbon are mixed according to the weight ratio of 2:10: 1.
The temperature of the decoloring tower is 100 ℃ and 120 ℃, and the vacuum degree is-0.097-0.099 kpa.
The switching frequency of the two filters is 30-48 hours/time.
In a deodorization working section, the temperature of a physical deacidification tower is reduced by 30-31 ℃ and controlled at 209 ℃ in addition to 208 ℃ and the temperature of heat-conducting oil is controlled at 218 ℃ in addition to strictly controlling and shortening the retention time and the vacuum degree of oil products in a system to be-0.097-0.099 MPa according to the characteristics of the linseed oil; and the retention time of the oil product in the deodorization system is controlled by properly increasing the feed flow of the deodorization system. Therefore, trans-fatty acid (TFA) which is easily generated at high temperature originally cannot be generated for an effective time, and the content of the linolenic acid in the oil product is reserved to the maximum extent.
The invention sets the deodorization tower as a double-layer tray, the temperature of the deacidification tower is reduced by 30-31 ℃, the temperature is controlled to be in the range of 208 plus 209 ℃, the temperature of the heat transfer oil is controlled to be in the range of 216 plus 218 ℃, the retention time of the oil product in the deodorization tower is strictly controlled to be shortened, the temperature is reduced from about 60 minutes to about 35-38 minutes, the vacuum degree is in the range of-0.097 to 0.099MPa, the feeding flow of the deodorization tower is increased, the feeding amount is increased from 3 tons/hour to 3.1-3.2 tons/hour, and the linolenic acid content in the produced linseed oil is obviously increased by 6-10 percent.
The invention has the advantages that: the consumption of clay and charcoal is obviously reduced, the oil production efficiency is high, the production period is short, the oil loss is low, and the cost advantage is obvious; from the aspect of investment, the process has no new modification requirement on equipment, and is easier to popularize and apply; according to the analysis of product quality indexes, the linolenic acid content of the first-grade finished oil under the two processes is obviously different, the linolenic acid content of the linseed oil in the process is obviously 6% -10% higher, trans-fatty acid which is unfavorable for health is obviously reduced, and the economic benefit is obvious.
The present invention will be further described with reference to the following specific examples.
Detailed Description
The following description of the preferred embodiments of the present invention is provided for the purpose of illustration and description, and is in no way intended to limit the invention.
The percent in the present invention means mass percent unless otherwise specified; but the percentage of the solution, unless otherwise specified, means that 100ml of the solution contains several grams of solute; the percentage between the liquids refers to the ratio of the volumes at 20 ℃.
Example 1
A process for effectively increasing the content of linolenic acid in refined vegetable oil comprises a decoloring section and a deodorizing section;
the specific operation of the decoloring section is as follows:
the crude oil degummed by hydration or the crude oil without glue in the raw material is heated to 100-120 ℃ by a steam heater, the effect is that the crude oil reaches the temperature point with good clay activity and strong adsorption capacity, the traditional temperature is 90-115 ℃, and the stripping load of a rear-section deodorization working section is lightened by slightly improving the refining depth; then before the pre-mixer is stirred and mixed with the white clay and the active carbon, firstly adding a filter aid such as perlite into an adsorbent (the dosage of the adsorbent is determined according to the actual production condition, sampling and analyzing are carried out every hour, and the tank charging frequency of the adsorbent is reduced when the color is qualified), so that the perlite, the white clay and the active carbon (the white clay bulk density is 0.70g/mL, the perlite bulk density is 0.18g/mL and the active carbon bulk density is 0.31g/mL) are mixed according to the different characteristics and the different advantages and disadvantages expressed in use according to the weight ratio of 2:10:1, and the combined adsorbent with the moderate bulk density after mixing is adopted, because the particle sizes are different, the surfaces of larger perlite particles are uneven and are extruded mutually, the surfaces are saw-toothed, and the perlite particles are mutually meshed and connected to form a rough filter gap, and a filter cake is formed on a filter plate, and simultaneously a more uniform filter cake can be provided for the other two kinds of adsorbent particles The bracket structure is even and loose, so that the void ratio of a finally formed filter cake is improved, higher continuous permeability is kept, and the adsorption capacity of the argil and the activated carbon can be utilized to the maximum extent, so that the switching period of a filter (a leaf filter) is prolonged, the dosage of an argil adsorbent is greatly reduced, the decoloring capacity is ensured, the dosage of the argil is reduced, and the oil is prevented from being stained with the taste of the argil in a decoloring process section; and then distilling some undesirable volatile light components in a decoloring tower with vacuumizing and steam to extract the light components from the top of the tower, pumping the oil mixed with the adsorbent at the bottom of the tower to a leaf filter through a pump at the bottom of the tower, wherein the filter is switched for use by two sets, and the clear oil filtered by the leaf filter enters a decoloring clear oil tank, temporarily stores the decolored clear oil after decoloring, and then enters the next working section, namely a dewaxing working section.
The concrete operation of the deodorization workshop section is as follows:
the dewaxed oil is heated by a heat exchanger, enters a gas separator for distillation, is pumped into an oil-oil heat exchanger, a (heat conduction oil) heater and is heated continuously, and is heated to 190-200 ℃ in a deodorization tower with the vacuum degree of not less than-0.096 Mpa, and simultaneously (a bottom quick valve of a second layer of tray of the deodorization tower is opened), so that the oil product which originally needs to pass through three layers of trays in the deodorization tower is reduced to only pass through an upper layer and a lower layer, the retention time of the oil product in high temperature is reduced, the retention time of the oil product which does not pass through a middle tray is 40 minutes after the bottom quick valve of the middle tray is opened, and the feeding amount (from 3 tons/hour) is increased to 3.1-3.2 tons/hour to; pumping the bottom of the deodorization tower into a physical deacidification tower, controlling the liquid level of the deacidification tower to be 0.06 m at the lowest limit, further reducing the retention time of oil products at high temperature, controlling the temperature to be 209-215 ℃, carrying out steam distillation under high vacuum, discharging free fatty acid and low molecular substances into a fatty acid catcher along with steam, pumping the bottom of the tower into an oil-oil heat exchanger for heat exchange and cooling, cooling a finished oil cooler, filtering the cooled finished oil by a polishing filter, and finally obtaining primary oil which is sent into a V-335 finished oil tank.
In a deodorization working section, the temperature of a physical deacidification tower is reduced by 30-31 ℃ and controlled at 209 ℃ and the temperature of heat-conducting oil is controlled at 218 ℃ according to the characteristics of the linseed oil, the retention time of oil products in a system (deodorization tower) is strictly controlled to be shortened (from about 60 minutes to about 35-38 minutes), and the vacuum degree (the vacuum degree of the whole deodorization system, including the vacuum degrees of a gas separator, the deodorization tower, the physical deacidification tower and a fatty acid catcher) is all-0.097-0.099 MPa; and controlling the retention time of the oil in the deodorization system by properly increasing the feed flow of the deodorization system (increasing the feed amount from 3 tons/hour to 3.1-3.2 tons/hour). Therefore, trans-fatty acid (TFA) which is easily generated at high temperature originally cannot be generated for an effective time, and the content of the linolenic acid in the oil product is reserved to the maximum extent.
The invention reduces the number of tower trays of the deodorization tower to be double-layer tower trays, controls the adjustment of temperature and retention time, and creates a novel combined adsorbent in a decoloring working section.
The results of comparing the conventional process with the new process are shown in Table 1 below:
the results of comparing the parameters of the conventional process and the new process are shown in the following table 2:
(first-grade linseed oil)
Parameter comparison result between traditional process and new process method
By comparing the process of the present invention with the conventional process, it can be seen from tables 1 and 2 that the process of the present invention significantly reduces the consumption of clay and activated carbon, while the perlite is only slightly increased. The oil production efficiency is high, the production period is short, the oil loss is low, and the cost advantage is obvious. From the analysis of investment, the process of the invention has no new modification requirement on equipment, and is easier to popularize and apply. And then, the analysis on the product quality indexes shows that the linolenic acid content of the first-grade finished oil under the two processes is obviously different, and the linolenic acid content in the linseed oil in the process is obviously higher by 6-10 percent. The trans-fatty acid which is unfavorable for health is obviously reduced to reach the undetected standard (according to the general rules of prepackaged food nutrition labels (GB28050-2011), the content of the trans-fatty acid in the food is less than or equal to 0.3g/100g (solid) or 100ml (liquid) and can be regarded as undetected), and the economic benefit is remarkable.
The raw materials used in the invention are common raw materials in the production in the field, can be obtained from the market, and do not influence the production result; the various devices adopted in the invention are conventional devices used in the production process in the field, and the operation, parameters and the like of each device are carried out according to the conventional operations without special points.
Claims (7)
1. A process capable of effectively improving the content of linolenic acid in refined vegetable oil is characterized in that: comprises a decoloring working section and a deodorizing working section;
the specific operation of the decoloring section is as follows: heating the crude oil degummed by hydration or the crude oil without glue in the raw material to 100-120 ℃ by a steam heater to reach the temperature point of good clay activity and strong adsorption capacity, and reducing the stripping load of a rear-section deodorization working section by improving the refining depth; then adding clay and activated carbon into filter aid perlite according to a certain proportion to form a new adsorbent, and stirring and mixing the crude oil and the adsorbent through a premixer; then distilling some non-ideal volatile light components in a decoloring tower with vacuumizing and steam to extract the light components from the top of the tower, pumping oil mixed with an adsorbent at the bottom of the tower to a filter through a pump at the bottom of the tower, wherein the filter is switched for use by two sets, and clear oil filtered by the filter enters a decoloring clear oil tank, temporarily stores the decolored clear oil, and then enters the next working section, namely a dewaxing working section;
the concrete operation of the deodorization workshop section is as follows: heating the dewaxed oil by a heat exchanger, distilling the dewaxed oil in a gas separator, pumping the dewaxed oil into an oil-oil heat exchanger and a heater, continuously heating the dewaxed oil, and heating the dewaxed oil to 190-200 ℃ in a deodorization tower with the vacuum degree of not less than-0.096 Mpa, so that the oil passes through an upper layer and a lower layer in the deodorization tower, the retention time is 40 minutes, and the treatment capacity is increased to 3.1-3.2 tons/hour; pumping the bottom of the deodorization tower into a physical deacidification tower, controlling the liquid level of the deacidification tower to be 0.06 m at the lowest limit, controlling the temperature to be 209-215 ℃, carrying out steam distillation under high vacuum to discharge free fatty acid and low molecular substances into a fatty acid catcher along with steam, pumping the bottom of the tower into an oil-oil heat exchanger for heat exchange and temperature reduction, cooling a finished oil cooler, filtering the cooled finished oil by a polishing filter to obtain primary oil, and sending the primary oil into a finished oil tank.
2. The process of claim 1, wherein the process is effective for increasing the linolenic acid content of a refined vegetable oil, and comprises: the deodorization tower and the physical deacidification tower adopt lower control temperature, and oil does not stay on a tower tray in the middle of the deodorization tower, so that the evaporation area and the stay volume of the deodorization tower are reduced by one third, the treatment capacity is increased, and the stay time is less than 40 minutes.
3. The process of claim 2, wherein the process is effective for increasing the linolenic acid content of a refined vegetable oil, and comprises: the oil product does not stay on the tower tray in the middle of the deodorization tower, and the method is to open a hand valve at the bottom of the deodorization tower tray to ensure that the oil product only passes through an upper layer and a lower layer in the deodorization tower.
4. The process of claim 1, wherein the process is effective for increasing the linolenic acid content of a refined vegetable oil, and comprises: bulk density of the clay: 0.70g/mL, bulk density of the perlite: 0.18g/mL, bulk density of the activated carbon: 0.31 g/mL.
5. The process of claim 1, wherein the process is effective for increasing the linolenic acid content of a refined vegetable oil, and comprises: the perlite, the argil and the activated carbon are mixed according to the weight ratio of 2:10: 1.
6. The process of claim 1, wherein the process is effective for increasing the linolenic acid content of a refined vegetable oil, and comprises: the temperature of the decoloring tower is 100 ℃ and 120 ℃, and the vacuum degree is-0.088 to-0.092 kpa.
7. The process of claim 1, wherein the process is effective for increasing the linolenic acid content of a refined vegetable oil, and comprises: the switching frequency of the two filters is 30-48 hours/time.
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| CN113698988A (en) * | 2021-07-27 | 2021-11-26 | 山东三星玉米产业科技有限公司 | Production process of nutritional corn oil |
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