CN108690716A - A kind of refining of maize oil production technology without dewaxing process - Google Patents
A kind of refining of maize oil production technology without dewaxing process Download PDFInfo
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- CN108690716A CN108690716A CN201810598296.XA CN201810598296A CN108690716A CN 108690716 A CN108690716 A CN 108690716A CN 201810598296 A CN201810598296 A CN 201810598296A CN 108690716 A CN108690716 A CN 108690716A
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Classifications
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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
- C11B3/02—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
-
- 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
-
- 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
- C11B7/0083—Separation of mixtures of fats or fatty oils into their constituents, e.g. saturated oils from unsaturated oils with addition of auxiliary substances, e.g. cristallisation promotors, filter aids, melting point depressors
Abstract
The invention belongs to edible oil and fat refining techniques fields, and in particular to a kind of refining of maize oil production technology without dewaxing process.The technique of the present invention includes following step:Alkali refining, decoloration, deodorization;Decolorization process includes primary decoloration and secondary decolourization.Refining of maize oil method provided by the present invention has broken traditional refinery practice, do not use individual hydrodewaxing step, but also complete the process of dewaxing simultaneously in decolorization process, the advantages of this technique is, reduce the discharge of the full use, steam of filter aid, reduce the input of equipment and saved due to energy consumption caused by dewaxing, while saving the use of human resources.
Description
Technical field
The invention belongs to edible oil and fat refining techniques fields, and in particular to a kind of refining of maize oil production without dewaxing process
Technique.
Background technology
Corn oil is also known as maize germ oil, Semen setariae oil, is the vegetable oil refined from the plumule of corn, containing it is abundant not
Saturated fatty acid, phytosterol, vitamin E and polyphenols.Corn germ fatty content is between 17%~45%, about
Account for 80% or more of corn total fats content.Aliphatic acid feature in corn oil be unsaturated fatty acid content be up to 80%~
85%.Corn oil itself does not contain cholesterol, it has dissolution for the accumulation of Blood Cholesterol, therefore can reduce to blood
Pipe generates hardening effect.There is positive preventive and therapeutic effect to geriatric disease such as artery sclerosis, diabetes etc..Due to natural compound
The function of vitamin E, to heart disease, thrombophlebitis, Reproductive Performance class obstacle, muscular atrophy, trophism encephalomalacia
There are apparent curative effect and prevention effect.Corn oil nutritive value is high, and the sense of taste is good, is unlikely to deteriorate, thus welcomed by the people.
American-European countries, corn oil are eaten extensively as a kind of table oil, enjoy " healthy oil ", " trusting oil ", " long life oil "
Etc. laudatory titles.
The nutrition of corn oil at present and its function affect gradually recognize receiving, production Technology by consumer
Development be also constantly subjected to pay close attention to and be constantly progressive, however there is also urgent problems to be solved:Energy consumption in refining process
Aspect is that very big, current refining of maize oil technique is also all confined to these workshop sections and be not improved.This there is
The problem of energy-saving aspect:In refining dewaxing process, it can be consumed during precoating, recycle, blowing cake, release, cake discharge etc.
The energy consumptions such as a series of electricity, gas.Just there is exhaust gas generation in workshop section itself, has a strand pungent taste, prodigious dirt is caused to air
Dye.So reducing the loss of dewaxing process energy consumption and the discharge of pollutant is just particularly important.
CN106906044A discloses a kind of method of refining reducing the toxic factor in corn oil, which is characterized in that including
Following steps:
1) alkali refining:It takes 1000 parts of raw corn oil first to clean, is heated to 80-85 DEG C and is mixed with 1.3 parts of phosphoric acid
After stopping 60-70 minute, then with 22.34 parts of the liquid caustic soda of 18-20 Baume degrees mix 2-3 minutes into the first desk centrifuge into
The de- soap of row takes off soap oil again with 22.34 parts of the liquid caustic soda of 8-10 Baume degrees, mixes 15-20 minutes;
2) secondary alkali refining:By step 1, treated that material puts into the second desk centrifuge again is taken off soap again, then and
After 50 parts of hot water, the mixing of 0.58 part of citric acid third desk centrifuge is entered to be washed, then enter back into drier into
Row drying enters bleaching process after dry;
3) it decolourizes:It is white with 24 parts by dry oil dried in above-mentioned steps 2 after being further heated to 105-110 DEG C
Soil, 1.9 parts of activated carbons, 7.25 parts of filter aid mixing carry out the native blending tank of oil, enter back into bleaching tower, 20-30 points are stopped in tower
Clock, be transported in filter be filtered, be cooled to 45-50 DEG C after enter dewaxing process.
4) it dewaxes:45-50 DEG C in above-mentioned steps 2 of decoloration edible vegetable oil is entered into dewaxing process:
Edible vegetable oil decolourize through further heat exchange, after temperature reaches 23-27 DEG C, is mixed into 3.85 parts of diatomite mixed to oily soil
It closing in tank, mixture is delivered to by delivery pump in crystallizing tank, and gradient heat exchange is carried out in crystallizing tank by refrigerator chilled water,
Oil 5 DEG C are cooled in 16 hours to crystallize;The decoloration edible vegetable oil temperature of advantages of good crystallization maintains 5 DEG C, starts to stand growing the grain 10-
12h;Then the good decoloration edible vegetable oil of growing the grain adds 1.5 parts of diatomite, is then input to and follows again after being delivered to precoating tank
Ring tank is applied to oil clearly in advance;Into in dewaxing edible vegetable oil tank, it is transported to deodorization procedures.
5) double tower dual temperature is deodorized:Dewaxing edible vegetable oil in above-mentioned steps 3 is reached into 60 DEG C of warps into one through further heat exchange, temperature
Step is heated to 95 DEG C, and subsequently into deodorization procedures gassing tank, a step enters deodorizing tower after being heated to 230-235 DEG C, in plate column
Interior stop 60-80 minutes is heated to 245-250 DEG C and enters filler extracting tower, is stopped 20-30 minutes in tower and goes out tower, warp
Heat exchange is cooled to 30 DEG C hereinafter, be filtered into finished pot using filter, takes the qualified input reservoir area storage of comprehensive sample chemical examination
It deposits.
In above method, corn oil first decolourizes to dewax again, it is necessary to pass through two different processes, and in dewaxing process not
It only needs to use special dewaxing device, and also needs to a large amount of energy consumption and manpower.
It, will necessarily without individual hydrodewaxing step is carried out again if it is dewaxing has also been completed at the same time during decoloration
Simplify production technology, saves dewaxing device and energy consumption.
Invention content
In order to solve the above technical problems, the present invention provides a kind of refining of maize oil of no hydrodewaxing step to produce work
Skill is saved to reach due to energy consumption caused by dewaxing process specifically, also completing dewaxing process simultaneously in decolorization process
Purpose, simplify technique.
In the present invention, the refining of maize oil production technology of no dewaxing process, including:Alkali refining, decoloration, deodorization;
In alkali refining step:Alkali refining time 35-80min, the additive amount of alkali is 0.2-0.4%, concentration of lye 16- in crude oil
19 ° of B é, alkali refining temperature are 75-95 DEG C.When alkali refining alkali refining (CN202181294U) is carried out with novel alkali time-retention tank;
Decolorization process includes:
Primary decoloration:It is decolourized using common process, decolorising agent is carclazyte and activated carbon, and the addition of carclazyte is to wait for bleached oil
The 1.8~2.6% of quality, the addition of activated carbon are the 0.05~0.15% of dry oil quality, decoloring reaction temperature is 110~
120 DEG C, the decoloring reaction time is 20~25min, and bleaching tower liquid level is 35~45%;
Secondary decolourization:First a part of bleached oil A of bleacher is delivered in crystallizing tank, remaining bleached oil B is retained in de-
In color tank, addition filter aid is added in bleached oil A;Stirring, bleached oil A after mixing, pass through crystallization coil pipe with filter aid
Crystallization temperature is controlled at 5~7 DEG C using chilled water, growing the grain temperature is 8~12 DEG C, and the time is 24~26 hours, then by institute
The crystal oil obtained is mixed with remaining bleached oil B, then adds atlapulgite, attapulgite and activated carbon, and decolourize 30-50min,
105-118 DEG C of bleaching temperature, is finally filtered.
In above decolorization process, filter aid is perlite or diatomite, and the addition of filter aid is 9~11 ‰.
Preferably, crystal oil and remaining bleached oil B are with 1:1 volume mixture.
Atlapulgite, attapulgite additive amount be respectively the 1.5~3% of crystal oil and remaining bleached oil B total volumes.
Activated carbon is preferably WY2 activated carbons, and additive amount is crystal oil with the 0.5 of remaining bleached oil B total volumes~
1.0‰。
Deodorization:Oil cycle is warming up to 240-260 DEG C, deodorization time 60-140min before into deodorizing tower, the vacuum of deodorizing tower
Spend 1.2-1.3bar, 245-260 DEG C of oil outlet temperature, oil into finished product dryer temperature be 100-108 DEG C.
Refining of maize oil method provided by the present invention has broken traditional refinery practice, is not walked using individually dewaxing
Suddenly, also complete the process of dewaxing but in decolorization process simultaneously, the advantages of this technique be the use for reducing filter aid,
It the discharge of steam, the input for reducing equipment and has saved due to energy consumption caused by dewaxing, while having saved human resources
Use.
Description of the drawings
Fig. 1 is the comparison figure of the corn oil and commercially available corn oil obtained by method through the invention.
Specific implementation mode
The present invention is further described with reference to specific embodiment, so that those skilled in the art knows more about
The present invention, but be not intended to limit the present invention.
Embodiment 1
Alkali refining alkali time-retention tank:CN202181294U, Shandong Sanxing Corn Technology Co., Ltd. provide;
When crude oil alkali refining, the additive amount of lye is the 0.3% of crude oil total weight, and concentration of lye is 17 ° of B é, and alkali refining temperature is
85℃。
The perlite or diatomite that a part of bleached oil is first squeezed into addition 10 ‰ in another tank, are stirred using crystallizing tank
It mixes, corn oil and filter aid after mixing, are controlled crystallization temperature at 6 DEG C using chilled water by crystallizing coil pipe, growing the grain temperature
At 10 DEG C, the time is 26 hours, and crystal oil and bleached oil are directly then carried out 1 for degree control:1 mixing is allowed to be formed one certainly
Right filter layer is crossed and adds atlapulgite 1.5%, attapulgite 1.5%, WY2 activated carbons in decoloration after time filter respectively again
0.6 ‰ (additive amount is the proportion for accounting for crystal oil and bleached oil gross weight volume), decolourize 40min, 115 DEG C of bleaching temperature, most
After be filtered.
Deodorization workshop section is warming up to 250 DEG C of (computer sensing display temperature into temperature (abbreviation D2A temperature) cycle oily before deodorizing tower
Degree) deodorization time is 100min, the vacuum degree 1.2bar of deodorizing tower, 255 DEG C of oil outlet temperature, oil is into finished product dryer temperature 105
℃。
Each index of corn oil extracted through the above refinery practice is as follows:
Index below be according to GB19111-2003 standard detection it is qualified (following embodiment herewith detection method)
The detections of the indices of acquisition is according to being respectively:Color and luster GB/T 22460-2008, acid value GB 5009.229-2016, moisture
And volatile matter GB 5009.236-2016, freezing experiment 17756-1999, VE and sterol content are the ginseng of corn oil nutritive index
Examine value):
Color and luster:Y13R1.3, acid value:0.097 (KOH) mg/g, peroxide value:0.22mmol/kg, moisture and volatile matter content:
0.01%, refrigeration test:0 DEG C of storage, 5.5 hours clears, VE contents:96mg/100g, sterol content:809mg/100g.
Comparative example 1
Alkali refining:When crude oil alkali refining, the additive amount of lye is the 0.3% of crude oil total weight, and concentration of lye is 17 ° of B é, alkali refining
Temperature is 85 DEG C of decolorations;
Decoloration:Decolorising agent is carclazyte and activated carbon, and the addition of carclazyte is to wait for bleached oil (obtained by previous production workshop section
Oil is also dry oil) quality 1.8~2.6%, the addition of activated carbon be the 0.05~0.15% of dry oil quality, decoloration
Reaction temperature is 110~120 DEG C, and the decoloring reaction time is 20~25min, and bleaching tower liquid level is 35~45%.
Dewaxing:50 DEG C or so of bleached oil is delivered to process:Bleached oil is through further heat exchange, after temperature reaches 25 DEG C,
Filter aid is added according to 10 ‰ ratio, filter aid is perlite (can also be diatomite), and mixture is conveyed by delivery pump
Into crystallizing tank, gradient heat exchange is carried out in crystallizing tank by refrigerator chilled water, will be tied using chilled water by crystallizing coil pipe
At 5 DEG C or so, growing the grain temperature is controlled at 10 DEG C or so, then by filter pump, by the good corn oil pump of growing the grain for brilliant temperature control
Enter and carry out precoating, is finally filtered.
Dewaxing crude maize oil is transported to by pumping in crystallizing tank, adds filter aid according to 10 ‰ ratio, filter aid is pearl
Rock or diatomite, are stirred using crystallizing tank, and corn oil after mixing, will be tied by crystallizing coil pipe using chilled water with filter aid
At 5 DEG C or so, growing the grain temperature is controlled at 10 DEG C or so, then by filter pump, by the good corn oil pump of growing the grain for brilliant temperature control
Enter and carry out precoating, is finally filtered.
Deodorization:Corn oil after purification is delivered to heat exchanger heating by pumping, is entered on stripper after being heated to 250 DEG C
Portion.Under the effect of gravity, by being moved down on tower, 250 DEG C of superheated steam is recycled, avoids steam anti-with free fatty
Answer, into tower bottom, gas moves from lower to upper, fully carries out heat exchange, under high vacuum state, vacuum degree 200pa with
Under.In bottom of tower, the corn oil of aggregation is conveyed by delivery pump, is condensed by three-level condenser, temperature is at 10 DEG C after condensation, last mistake
Filter pump enters tank field or packaging.
In comparative example 1, each index of corn oil extracted through the above refinery practice is as follows:
Index below is the qualified (indices obtained in following embodiment of standard detection according to GB19111-2003
Detection according to being respectively:Color and luster GB/T 22460-2008, acid value GB 5009.229-2016, moisture and volatile matter content GB
5009.236-2016, freezing experiment 17756-1999, VE and sterol content are the reference value of corn oil nutritive index):
Color and luster:Y20R2.0, acid value:0.13 (KOH) mg/g, peroxide value:0.51mmol/kg, moisture and volatile matter content:
0.03%, refrigeration test:0 DEG C of storage, 5.5 hours clears, VE contents:89mg/100g, sterol content:798mg/100g.
Conclusion:The present invention is can be seen that compared with the method before improvement from above data comparison, reduces dewaxing
Step also completes the process of dewaxing while decoloration;It need not have been saved due to produced by dewaxing again using the equipment of dewaxing
Energy consumption, to save cost, nor will produce the exhaust gas by dewaxing institute band, energy conservation and environmental protection.In the quality side of oil
Face more Zhuo Zhong, nutrient component damages rate reduce, and color and luster, freezing experiment etc. are preferably promoted.
Left in Fig. 1 is product oil of the method using the present invention to gained after corn oil progress alkali refining, decoloration, deodorization, Fig. 1
The middle right side is commercially available corn oil product, passes through the comparison of the two, it is found that the corn oil in the present invention is of light color and bright,
Its decolorizing effect is preferable.
Embodiment 2
When crude oil alkali refining, the 0.3% of total weight when the additive amount of lye is crude oil, concentration of lye is 18 ° of B é, alkali refining temperature
It is 85 DEG C.The perlite or diatomite that a part of bleached oil is first squeezed into addition 11 ‰ in another tank, are stirred using crystallizing tank,
Corn oil and filter aid after mixing, are controlled crystallization temperature at 6 DEG C using chilled water by crystallizing coil pipe, growing the grain temperature control
For system at 15 DEG C, the time is 25 hours, and crystal oil and bleached oil are directly then carried out 1:2 mixing are allowed to be formed one naturally
Filter layer adds atlapulgite, attapulgite 1.8% (additive amount), WY2 activated carbons in decoloration again after crossing time filter
0.6 ‰ (additive amounts), decolourize 40min, 118 DEG C of bleaching temperature.Finally it is filtered.Workshop section is deodorized into oily temperature before deodorizing tower
It is 80min, the vacuum degree of deodorizing tower that (abbreviation D2A temperature) cycle, which is warming up to 250 DEG C of (computer sensing displays temperature) deodorization times,
1.3bar, 255 DEG C of oil outlet temperature, oil is into 105 DEG C of finished product dryer temperature.
Each index of corn oil through the extraction of the above refinery practice is color and luster:Y10R1.0, acid value:0.15 (KOH) mg/g, mistake
Oxidation number:0.41mmol/kg, moisture and volatile matter content:0.01%, refrigeration test:0 DEG C of storage, 4.5 hours clears (do not conform to
Lattice), VE contents:91mg/100g, sterol content:803mg/100g.
Embodiment 3
When crude oil alkali refining, the 0.3% of total weight when the additive amount of lye is crude oil, concentration of lye is 18 ° of B é, alkali refining temperature
It is 75 DEG C.The perlite or diatomite that a part of bleached oil is first squeezed into addition 11 ‰ in another tank, are stirred using crystallizing tank,
Corn oil and filter aid after mixing, are controlled crystallization temperature at 6 DEG C using chilled water by crystallizing coil pipe, growing the grain temperature control
For system at 12 DEG C, the time is 24 hours, and crystal oil and bleached oil are directly then carried out 1:1 mixing is allowed to be formed one naturally
Filter layer adds atlapulgite, attapulgite 2.1% (additive amount), WY2 activated carbons in decoloration again after crossing time filter
0.8 ‰ (additive amounts), decolourize 40min, 108 DEG C of bleaching temperature.Finally it is filtered.Workshop section is deodorized into oily temperature before deodorizing tower
It is 80min, the vacuum degree of deodorizing tower that (abbreviation D2A temperature) cycle, which is warming up to 260 DEG C of (computer sensing displays temperature) deodorization times,
1.3bar, 250 DEG C of oil outlet temperature, oil is into 106 DEG C of finished product dryer temperature.
Each index of corn oil through the extraction of the above refinery practice is color and luster:Y12R1.2, acid value:0.10 (KOH) mg/g, mistake
Oxidation number:0.36mmol/kg, moisture and volatile matter content:0.02%, refrigeration test:0 DEG C of storage, 5.5 hours clears, VE contain
Amount:92mg/100g, sterol content:821mg/100g.
Claims (9)
1. a kind of refining of maize oil production technology without dewaxing process, it is characterised in that:The technique includes:Alkali refining, takes off decoloration
It is smelly;
Decolorization process includes:
Primary decoloration:It is decolourized using conventional method:Decolorising agent is added in waiting for bleached oil and carries out decoloring reaction, obtains bleached oil A;
Secondary decolourization:First a part of bleached oil A of bleacher is delivered in crystallizing tank, remaining bleached oil B is retained in bleacher
In, addition filter aid is added in bleached oil A;Stirring, bleached oil A and filter aid after mixing, control crystallization temperature is 5~
7 DEG C, growing the grain temperature is 8~12 DEG C, and the time is 24~26 hours, then mixes the crystal oil of gained with remaining bleached oil B,
Atlapulgite, attapulgite and activated carbon are added again, and decolourize 30-50min, and 105-118 DEG C of bleaching temperature finally filters.
2. the refining of maize oil production technology as described in claim 1 without dewaxing process, which is characterized in that it is characterized in that,
Filter aid is perlite or diatomite, and the addition of filter aid is 9~11 ‰.
3. the refining of maize oil production technology as described in claim 1 without dewaxing process, which is characterized in that it is characterized in that,
Crystal oil is with remaining bleached oil B with 1:1 volume mixture.
4. the refining of maize oil production technology as described in claim 1 without dewaxing process, which is characterized in that it is characterized in that,
Atlapulgite, attapulgite additive amount be respectively the 1.5~3% of crystal oil and remaining bleached oil B total volumes.
5. the refining of maize oil production technology as described in claim 1 without dewaxing process, which is characterized in that it is characterized in that,
Activated carbon is WY2 activated carbons, and additive amount is 0.5~the 1.0 ‰ of crystal oil and remaining bleached oil B total volumes.
6. the refining of maize oil production technology as described in claim 1 without dewaxing process, which is characterized in that it is characterized in that,
Alkali refining:Alkali refining time 35-80min, the additive amount of alkali is 0.2-0.4% in crude oil, and concentration of lye is 16-19 ° of B é, alkali refining temperature
It is 75-95 DEG C.
7. the refining of maize oil production technology as described in claim 1 without dewaxing process, which is characterized in that deodorization:Into deodorization
Oil cycle is warming up to 240-260 DEG C, deodorization time 60-140min before tower, and the vacuum degree 1.2-1.3bar of deodorizing tower goes out oil temperature
Degree 245-260 DEG C, oil into finished product dryer temperature be 100-108 DEG C.
8. the refining of maize oil production technology as described in claim 1 without dewaxing process, which is characterized in that
Crystallization temperature is controlled at 5~7 DEG C using chilled water by crystallizing coil pipe.
9. the refining of maize oil production technology as described in claim 1 without dewaxing process, which is characterized in that
In primary decoloration, decolorising agent is carclazyte and activated carbon, and the addition of carclazyte is the 1.8~2.6% of oil quality to be decolourized, living
Property charcoal addition be the 0.05~0.15% of dry oil quality, decoloring reaction temperature is 110~120 DEG C, the decoloring reaction time
For 20~25min, bleaching tower liquid level is 35~45%.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112831371A (en) * | 2019-11-24 | 2021-05-25 | 湖南大三湘茶油股份有限公司 | High-quality colorless tea oil and preparation method thereof |
| 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 |
| CN113698988B (en) * | 2021-07-27 | 2024-04-26 | 长寿花食品股份有限公司 | Production process of nutritional corn oil |
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| CN113698988B (en) * | 2021-07-27 | 2024-04-26 | 长寿花食品股份有限公司 | Production process of nutritional corn oil |
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