CN109609264A - A kind of refinery practice improving corn oil quality - Google Patents
A kind of refinery practice improving corn oil quality Download PDFInfo
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- CN109609264A CN109609264A CN201910116367.2A CN201910116367A CN109609264A CN 109609264 A CN109609264 A CN 109609264A CN 201910116367 A CN201910116367 A CN 201910116367A CN 109609264 A CN109609264 A CN 109609264A
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- 235000005687 corn oil Nutrition 0.000 title claims abstract description 74
- 239000002285 corn oil Substances 0.000 title claims abstract description 34
- 239000003921 oil Substances 0.000 claims abstract description 139
- 235000019198 oils Nutrition 0.000 claims abstract description 139
- 239000002253 acid Substances 0.000 claims abstract description 59
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 38
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 30
- 238000000034 method Methods 0.000 claims abstract description 29
- 239000000047 product Substances 0.000 claims abstract description 26
- 239000012065 filter cake Substances 0.000 claims abstract description 22
- 238000009874 alkali refining Methods 0.000 claims abstract description 19
- 238000004332 deodorization Methods 0.000 claims abstract description 19
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 15
- 230000014759 maintenance of location Effects 0.000 claims abstract description 12
- 238000007670 refining Methods 0.000 claims abstract description 10
- 238000001914 filtration Methods 0.000 claims abstract description 8
- 238000004061 bleaching Methods 0.000 claims description 19
- GVJHHUAWPYXKBD-UHFFFAOYSA-N (±)-α-Tocopherol Chemical compound OC1=C(C)C(C)=C2OC(CCCC(C)CCCC(C)CCCC(C)C)(C)CCC2=C1C GVJHHUAWPYXKBD-UHFFFAOYSA-N 0.000 claims description 18
- MBMQEIFVQACCCH-UHFFFAOYSA-N trans-Zearalenon Natural products O=C1OC(C)CCCC(=O)CCCC=CC2=CC(O)=CC(O)=C21 MBMQEIFVQACCCH-UHFFFAOYSA-N 0.000 claims description 15
- MBMQEIFVQACCCH-QBODLPLBSA-N zearalenone Chemical compound O=C1O[C@@H](C)CCCC(=O)CCC\C=C\C2=CC(O)=CC(O)=C21 MBMQEIFVQACCCH-QBODLPLBSA-N 0.000 claims description 15
- 238000012545 processing Methods 0.000 claims description 14
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 12
- 229960000892 attapulgite Drugs 0.000 claims description 12
- 238000011049 filling Methods 0.000 claims description 12
- 239000000463 material Substances 0.000 claims description 12
- 229910052625 palygorskite Inorganic materials 0.000 claims description 12
- 239000010779 crude oil Substances 0.000 claims description 11
- 238000003756 stirring Methods 0.000 claims description 10
- 229930003427 Vitamin E Natural products 0.000 claims description 9
- WIGCFUFOHFEKBI-UHFFFAOYSA-N gamma-tocopherol Natural products CC(C)CCCC(C)CCCC(C)CCCC1CCC2C(C)C(O)C(C)C(C)C2O1 WIGCFUFOHFEKBI-UHFFFAOYSA-N 0.000 claims description 9
- 235000019165 vitamin E Nutrition 0.000 claims description 9
- 229940046009 vitamin E Drugs 0.000 claims description 9
- 239000011709 vitamin E Substances 0.000 claims description 9
- 238000002156 mixing Methods 0.000 claims description 8
- 229910001220 stainless steel Inorganic materials 0.000 claims description 8
- 239000010935 stainless steel Substances 0.000 claims description 8
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 6
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 6
- 235000013305 food Nutrition 0.000 claims description 6
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 6
- 238000012546 transfer Methods 0.000 claims description 6
- 238000010792 warming Methods 0.000 claims description 6
- WRIDQFICGBMAFQ-UHFFFAOYSA-N (E)-8-Octadecenoic acid Natural products CCCCCCCCCC=CCCCCCCC(O)=O WRIDQFICGBMAFQ-UHFFFAOYSA-N 0.000 claims description 5
- LQJBNNIYVWPHFW-UHFFFAOYSA-N 20:1omega9c fatty acid Natural products CCCCCCCCCCC=CCCCCCCCC(O)=O LQJBNNIYVWPHFW-UHFFFAOYSA-N 0.000 claims description 5
- QSBYPNXLFMSGKH-UHFFFAOYSA-N 9-Heptadecensaeure Natural products CCCCCCCC=CCCCCCCCC(O)=O QSBYPNXLFMSGKH-UHFFFAOYSA-N 0.000 claims description 5
- ZQPPMHVWECSIRJ-UHFFFAOYSA-N Oleic acid Natural products CCCCCCCCC=CCCCCCCCC(O)=O ZQPPMHVWECSIRJ-UHFFFAOYSA-N 0.000 claims description 5
- 239000005642 Oleic acid Substances 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 5
- QXJSBBXBKPUZAA-UHFFFAOYSA-N isooleic acid Natural products CCCCCCCC=CCCCCCCCCC(O)=O QXJSBBXBKPUZAA-UHFFFAOYSA-N 0.000 claims description 5
- ZQPPMHVWECSIRJ-KTKRTIGZSA-N oleic acid Chemical compound CCCCCCCC\C=C/CCCCCCCC(O)=O ZQPPMHVWECSIRJ-KTKRTIGZSA-N 0.000 claims description 5
- 229930182558 Sterol Natural products 0.000 claims description 4
- 230000003647 oxidation Effects 0.000 claims description 4
- 238000007254 oxidation reaction Methods 0.000 claims description 4
- 150000003432 sterols Chemical class 0.000 claims description 4
- 235000003702 sterols Nutrition 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 235000010692 trans-unsaturated fatty acids Nutrition 0.000 claims description 3
- 238000005119 centrifugation Methods 0.000 claims description 2
- 238000010025 steaming Methods 0.000 claims 1
- 239000004615 ingredient Substances 0.000 abstract description 7
- 238000004042 decolorization Methods 0.000 abstract description 6
- 230000006378 damage Effects 0.000 abstract description 5
- 235000016709 nutrition Nutrition 0.000 abstract description 5
- 239000002994 raw material Substances 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 235000008935 nutritious Nutrition 0.000 abstract description 2
- 235000014593 oils and fats Nutrition 0.000 abstract description 2
- 230000001737 promoting effect Effects 0.000 abstract description 2
- 230000009467 reduction Effects 0.000 abstract description 2
- 239000002671 adjuvant Substances 0.000 abstract 1
- 230000008569 process Effects 0.000 description 13
- 238000007664 blowing Methods 0.000 description 8
- 238000002474 experimental method Methods 0.000 description 8
- 238000007710 freezing Methods 0.000 description 8
- 230000008014 freezing Effects 0.000 description 8
- 240000008042 Zea mays Species 0.000 description 5
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 5
- 238000011109 contamination Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 235000016383 Zea mays subsp huehuetenangensis Nutrition 0.000 description 4
- 230000008859 change Effects 0.000 description 4
- 239000004927 clay Substances 0.000 description 4
- 239000013078 crystal Substances 0.000 description 4
- 239000000314 lubricant Substances 0.000 description 4
- 235000009973 maize Nutrition 0.000 description 4
- 210000001161 mammalian embryo Anatomy 0.000 description 4
- 238000010561 standard procedure Methods 0.000 description 4
- 239000004519 grease Substances 0.000 description 2
- 230000036541 health Effects 0.000 description 2
- 230000035764 nutrition Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000003053 toxin Substances 0.000 description 2
- 231100000765 toxin Toxicity 0.000 description 2
- 108700012359 toxins Proteins 0.000 description 2
- 235000021122 unsaturated fatty acids Nutrition 0.000 description 2
- 150000004670 unsaturated fatty acids Chemical class 0.000 description 2
- 206010003211 Arteriosclerosis coronary artery Diseases 0.000 description 1
- OYHQOLUKZRVURQ-HZJYTTRNSA-N Linoleic acid Chemical compound CCCCC\C=C/C\C=C/CCCCCCCC(O)=O OYHQOLUKZRVURQ-HZJYTTRNSA-N 0.000 description 1
- 206010067171 Regurgitation Diseases 0.000 description 1
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- FPQFYIAXQDXNOR-QDKLYSGJSA-N alpha-Zearalenol Chemical compound O=C1O[C@@H](C)CCC[C@H](O)CCC\C=C\C2=CC(O)=CC(O)=C21 FPQFYIAXQDXNOR-QDKLYSGJSA-N 0.000 description 1
- 230000003064 anti-oxidating effect Effects 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 235000005822 corn Nutrition 0.000 description 1
- 208000029078 coronary artery disease Diseases 0.000 description 1
- 230000001877 deodorizing effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 239000002158 endotoxin Substances 0.000 description 1
- 239000003925 fat Substances 0.000 description 1
- 235000019197 fats Nutrition 0.000 description 1
- 239000000194 fatty acid Substances 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 235000020778 linoleic acid Nutrition 0.000 description 1
- OYHQOLUKZRVURQ-IXWMQOLASA-N linoleic acid Natural products CCCCC\C=C/C\C=C\CCCCCCCC(O)=O OYHQOLUKZRVURQ-IXWMQOLASA-N 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000008204 material by function Substances 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 235000019871 vegetable fat Nutrition 0.000 description 1
- 229960002300 zeranol Drugs 0.000 description 1
Classifications
-
- 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
- C11B3/001—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
- C11B3/008—Refining fats or fatty oils by filtration, e.g. including ultra filtration, dialysis
-
- 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
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Microbiology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Fats And Perfumes (AREA)
Abstract
The invention discloses a kind of refinery practices for improving corn oil quality, belong to corn oil manufacture field, comprising steps of 1) balanced crude maize oil acid value, 2) alkali refining, 3) dewaxing, 4) decoloration, filtering, 5) deodorization, 6) finished product nitrogen charging.Technique proposed by the present invention, decolorising agent dosage is small in decolorization, reduces bleached oil acid value and increases, improve α-VE retention rate, at the same filter sump oil can reuse, filter cake Residual oil is low, bleached oil yield is improved, pollution problem of the bad smell of useless decolorising agent generation to environment is mitigated.The present invention, which changes east of oil and returned color value by raw material difference bring, fluctuates big limitation, the oil product of acquisition is better than national standard, improve the nutritious retention rate in oil product Central Plains, the farthest content of harm reduction ingredient, adjuvant consumption is low, appropriateness refining reduces the destruction to nutritional ingredient, is suitable for promoting and applying in Oils and fats enterprise.
Description
Technical field
Grease can be effectively controlled the invention belongs to corn oil manufacture field more particularly to one kind and return color, sour regurgitation, reduce corn
Zeranol toxin, the refining of maize oil technique for improving nutritional ingredient.
Background technique
Corn oil belongs to nutrient health vegetable fat of the rich containing physiologically active ingredient, is to process to make by maize
, maize germ oil can also be referred to as.Corn oil contains 86% or so unsaturated fatty acid, and wherein linoleic acid content is most
Height is 56% or so.Although corn oil unsaturated fatty acid is higher, since corn oil is rich in good antioxidation
Functional materials vitamin E, phytosterol, so that it has, stability is good, is not easy the spy being oxidized, the shelf-life is relatively long
Point.In addition to this, because its character is transparent, pale yellow, it is suitble to cook, fries, decoct, frying, non-greasy, long-term consumption can be effectively pre-
The generation of anti-coronary heart disease and artery sclerosis, and the public favor and concern gradually increased by health care consciousness.
The processing of traditional corn oil: the methods of squeezing, leaching is mostly used to extract crude maize oil, because of the maize raw material place of production, time
And processing technology is different, causes the nutriments such as crude maize oil color, acid value, VE, phytosterol, harmful substance content of toxins poor
It is different larger.Produce that public nutrition content of interest is stable, endangering ingredient, low, shelf color becomes for crude oil refining
The corn oil for changing small high-quality brings certain technical problem.Traditional polished fat's technique: it mostly uses degumming, depickling, take off
Color, dewaxing and deodorizing technology process obtain corn oil.Since each process reaction temperature is high, the reaction time is long, repeatedly for a long time
It is raised to higher temperature from low temperature, causes the overrefinement of corn oil, and destroys original nutriment or the substance that causes damages
Increase, is unfavorable for the stabilization of oil quality.Although with advances in technology, can obtain using different technique and meet country
The corn oil of standard, but can solve the problems, such as simultaneously due to maize raw material bring endotoxin contamination, VE content caused by overrefinement,
Sterol content reduces, and trans-fatty acid increases, and accelerated oxidation acid value is high, shelf life color deepens that i.e. grease " returning color " value is high asks
Topic, to obtain, nutrition content is stable, endangering ingredient, low, shelf color changes small high-quality corn oil, becomes each oil
Rouge enterprise technical problem urgently to be resolved.
Summary of the invention
In order to overcome the drawbacks of the prior art, the present invention provides a kind of refinery practices for improving corn oil quality.
Specifically the present invention adopts the following technical scheme: a kind of refinery practice for improving corn oil quality, which is characterized in that institute
Technique is stated to specifically comprise the following steps:
1) balanced crude maize oil acid value: before refining of maize oil processing, crude maize oil is placed in crude maize oil storage tank, is used
Pressure is 6Kg/cm2Compressed air stir 5min, so that whole tank crude maize oil acid value is reached unanimity；
2) alkali refining: it will be pumped into crude oil processing tank through oil transfer pump through step 1) treated crude maize oil, will be filtered through filter
Afterwards, then through heat exchanger 50 DEG C~60 DEG C are heated to, the food grade phosphoric acid of concentration 70%~80% is added, the acid after controlling acid adding
Value, the value added of acid value are less than 0.15mgKOH/g, react 20min~30min, and acid treated corn oil and 12 Baume degrees~
The liquid alkaline of 16 Baume degrees reacts 15min~20min at 70 DEG C~80 DEG C, is separated through centrifugation apparatus, obtained alkali refining oil
Acid value control is in 0.15mgKOH/g hereinafter, saponified matter content≤200ppm, phosphorous≤5ppm, zearalenone removal efficiency reach
35% or more；
3) dewax: alkali refining oil is delivered in filter aid premixing tank after heat exchanger exchanges heat to 30 DEG C, to filter aid premixing tank
The interior diatomite that oil is added and weighs 3 ‰~4 ‰ after the completion of premix, is pumped into the continuous crystallizing tank of temperature formula setting in gradient, with 3 DEG C/
The cooling of h~4 DEG C/h speed, temperature enter maturator after dropping to 4 DEG C~6 DEG C and keep the temperature 24 hours, and oil temperature is then raised to 13 DEG C
~15 DEG C are filtered, and obtain dewaxed oil；
4) decolourize, filter: dewaxed oil after heat exchanger exchanges heat to 110 DEG C enter decolorising agent premixing tank, be added decolorising agent with
Mixing, decolorising agent includes carclazyte and attapulgite, and the quality proportioning of carclazyte and attapulgite is (3~4): 1, be pumped into after mixing
Bleaching tower, 95 DEG C~105 DEG C of reaction temperature, decolourize 20min~30min, obtained bleached oil acid value 0.18mgKOH/g~
0.20mgKOH/g, color Y20, R2.9~3.1,88%~90%, zearalenone removal efficiency reaches vitamin E retention rate
To 30% or more, filtering is 4Kg/cm in pressure2Pressure condition under nitrogen blow cake 10min~15min, the dirt of filter cake blowout
Oil is pumped into bleaching tower, sump oil color Y20, R2.9~3.1, filter cake Residual oil≤18% through slop tank；
5) be deodorized: bleached oil is warming up to 238 DEG C~240 DEG C, into deodorization plate tower, 230 DEG C of tower exit temperature, reacts 30min,
Be pumped into deodorization filling material tower under conditions of steam pressure is 0.04MPa~0.06MPa, react 5min, 0.012MPa~
Deodorization filling material tower is discharged under 0.014MPa pressure at expulsion, tower exit temperature is cooled to 28 DEG C at 228 DEG C~230 DEG C, through heat exchanger, pump
Enter product oil stainless steel storage tank, for vitamin E retention rate 75% or more, finished product oil index meets GB19111-2017 primary oil
Standard, 120 DEG C, 8h returns color, color Y20, R2.9~3.2；105 DEG C of accelerated oxidation acid values are less than 0.1mgKOH/g, α-VE phase
Equivalent in 25mg/100g~28mg/100g, content of trans fatty acids less than 0.2%, zearalenone content 25ppb with
Under, sterol content is in 680mg/kg or more；
6) nitrogen charging: product oil is filled with nitrogen after entering product oil stainless steel storage tank, guarantees corn oil quality.
Through the above design, the present invention can be brought the following benefits:
1, technique proposed by the present invention, decolorising agent dosage is small in decolorization, reduces bleached oil acid value and increases, improves α-
VE retention rate, at the same filter sump oil can reuse, filter cake Residual oil is low, improves bleached oil yield, mitigate useless decolorising agent generate it is bad
Pollution problem of the smell to environment.
2, the present invention, which changes east of oil and returned color value by raw material difference bring, fluctuates big limitation, the oil product of acquisition
Better than national standard, the nutritious retention rate in oil product Central Plains is improved, farthest the content of harm reduction ingredient, auxiliary
Agent consumption is low, and appropriateness refining reduces the destruction to nutritional ingredient, is suitable for promoting and applying in Oils and fats enterprise.
Specific embodiment
In order to illustrate more clearly of the present invention, below with reference to preferred embodiment, the present invention is described further.Ability
Field technique personnel should be appreciated that following specifically described content is illustrative and be not restrictive, this should not be limited with this
The protection scope of invention.
The finished product oil index obtained through present invention process meets GB19111-2017 level-one oil standard, and 120 DEG C, 8h is returned
Color, color Y20, R2.9~3.2；105 DEG C of accelerated oxidation acid values are less than 0.1mgKOH/g, α-VE equivalent 25mg/100g~
28mg/100g, content of trans fatty acids is less than 0.2%, and zearalenone content is in 25ppb hereinafter, sterol content exists
680mg/kg or more.
Embodiment 1
The refinery practice that corn oil quality is improved in the present embodiment, includes the following steps:
Step 1: balanced crude maize oil acid value: before refining of maize oil processing, crude maize oil being placed in crude maize oil storage tank
It is interior, use pressure for 6Kg/cm2Compressed air stir 5min, so that whole tank crude maize oil is in upper and lower level and seethe state, to reach
It is at equilibrium to lubricant component, acid value；
Step 2: alkali refining: the crude maize oil after balanced is pumped into crude oil processing tank through oil transfer pump, after filter filters, then
55 DEG C are heated to through heat exchanger, the food grade phosphoric acid of concentration 70% is added, the acid value after controlling acid adding, the value added of acid value is less than
0.15mgKOH/g reacts 20min, and the liquid alkaline of acid treated corn oil and 12 Baume degrees reacts 15min at 70 DEG C, through from
Heart equipment is separated, and obtained alkali refining oleic acid value is controlled in 0.15mgKOH/g hereinafter, saponified matter content≤200ppm, phosphorous≤
5ppm, zearalenone removal efficiency reach 36%；
Step 3: dewaxing: alkali refining oil is delivered in filter aid premixing tank after heat exchanger exchanges heat to 30 DEG C, pre- to filter aid
It mixes and the diatomite that oil weighs 3 ‰ is added in tank, after the completion of premix, the continuous crystallizing tank of temperature formula setting in gradient is pumped into, with 3 DEG C/h
The speed of~4 DEG C/h cools down, and temperature enters maturator after dropping to 4 DEG C~6 DEG C and keeps the temperature 24 hours, then by oil temperature be raised to 13 DEG C into
Row filtering, obtains dewaxed oil；
The generally existing filter aid additional amount of existing dewaxing technique is high, and oil loss is serious, and the dewaxing freezing experiment time is short to ask
Topic reduces filter aid dosage the invention can ensure that crystal grain straight uniform, improves oil yield, dewaxed oil freezing experiment up to 48h with
On；
Step 4: dewaxed oil enters decolorising agent premixing tank after heat exchanger exchanges heat to 110 DEG C, decolorising agent is added and mixes therewith
It closes, decolorising agent includes carclazyte and attapulgite, and the quality proportioning of carclazyte and attapulgite is 3:1, bleaching tower is pumped into after mixing, instead
Answer 95 DEG C of temperature, decolourize 20min, obtained bleached oil acid value in 0.18mgKOH/g~0.20mgKOH/g, color Y20, R3.1,
Filtering, for vitamin E retention rate 90%, zearalenone removal efficiency reaches 32%, is 4Kg/cm in pressure2Pressure condition
Lower nitrogen blows cake 10min, and the sump oil of filter cake blowout is pumped into bleaching tower through slop tank, sump oil color Y20, R3.1, filter cake Residual oil
18%；
The existing generally existing decolorising agent dosage of decoloration process is big, and spent bleaching clay Residual oil is high, and bleached oil acid value increases higher, filter cake
Sump oil color out is deeper, it is more difficult to which the problem of increase of bleached oil color is caused after reuse or reuse, the present invention is in decolorization
Middle removal steam-stirring, steam blowing filter cake, it is ensured that the stability of bleached oil color manipulation, less decolorising agent usage amount change
It is apt to the odor contamination generated when blowing cake, reduces useless decolorising agent resid amount, improve bleaching workshop section yield, mitigates the decolorising agent that gives up to environment
Pollution problem；
Step 5: bleached oil is warming up to 240 DEG C, into deodorization plate tower, 230 DEG C of tower exit temperature, 30min is reacted, in steam
Pressure is pumped into deodorization filling material tower under conditions of being 0.04MPa, reacts 5min, deodorization filling material is discharged under 0.012MPa pressure at expulsion
Tower, tower exit temperature are cooled to 28 DEG C at 228 DEG C, through heat exchanger, are pumped into product oil stainless steel storage tank, are filled with 99.99% after tank is full
High pure nitrogen guarantees corn oil quality to reduce contact of the product oil with air to greatest extent.
Embryo is mentioned using wet process in the present embodiment, the crude oil that squeezing process obtains, acid value AV 4.3mgKOH/g~
The product oil of 5.0mgKOH/g, acquisition are detected using national standard method, and as follows: index is shown in Table 1.
Embodiment 2
The refinery practice that corn oil quality is improved in the present embodiment, includes the following steps:
Step 1: balanced crude maize oil acid value: before refining of maize oil processing, crude maize oil being placed in crude maize oil storage tank
It is interior, use pressure for 6Kg/cm2Compressed air stir 5min, so that whole tank crude maize oil is in upper and lower level and seethe state, to reach
It is at equilibrium to lubricant component, acid value；
Step 2: alkali refining: the crude maize oil after balanced is pumped into crude oil processing tank through oil transfer pump, after filter filters, then
60 DEG C are heated to through heat exchanger, the food grade phosphoric acid of concentration 75% is added, the acid value after controlling acid adding, the value added of acid value is less than
0.15mgKOH/g reacts 20min, and the liquid alkaline of acid treated corn oil and 14 Baume degrees reacts 15min at 75 DEG C, through from
Heart equipment is separated, and obtained alkali refining oleic acid value is controlled in 0.15mgKOH/g hereinafter, saponified matter content≤200ppm, phosphorous≤
5ppm, zearalenone removal efficiency reach 37%；
Step 3: dewaxing: alkali refining oil is delivered in filter aid premixing tank after heat exchanger exchanges heat to 30 DEG C, pre- to filter aid
It mixes and the diatomite that oil weighs 3.5 ‰ is added in tank, after the completion of premix, the continuous crystallizing tank of temperature formula setting in gradient is pumped into, with 3
DEG C/h~4 DEG C/h speed cooling, temperature drop to 4 DEG C~6 DEG C after enter maturator keep the temperature 24 hours, oil temperature is then raised to 14
It DEG C is filtered, obtains dewaxed oil；
The generally existing filter aid additional amount of existing dewaxing technique is high, and oil loss is serious, and the dewaxing freezing experiment time is short to ask
Topic reduces filter aid dosage the invention can ensure that crystal grain straight uniform, improves oil yield, dewaxed oil freezing experiment up to 48h with
On；
Step 4: dewaxed oil enters decolorising agent premixing tank after heat exchanger exchanges heat to 110 DEG C, decolorising agent is added and mixes therewith
It closes, decolorising agent includes carclazyte and attapulgite, and the quality proportioning of carclazyte and attapulgite is 3:1, bleaching tower is pumped into after mixing, instead
Answer 100 DEG C of temperature, decolourize 25min, obtained bleached oil acid value in 0.18mgKOH/g~0.20mgKOH/g, color Y20,
R2.9, filtering, for vitamin E retention rate 88%, zearalenone removal efficiency reaches 31%, is 4Kg/cm in pressure2Pressure
Nitrogen blows cake 12min under the conditions of power, and the sump oil of filter cake blowout is pumped into bleaching tower through slop tank, sump oil color Y20, R2.9, filter cake
Residual oil 18%；
The existing generally existing decolorising agent dosage of decoloration process is big, and spent bleaching clay Residual oil is high, and bleached oil acid value increases higher, filter cake
Sump oil color out is deeper, it is more difficult to which the problem of increase of bleached oil color is caused after reuse or reuse, the present invention is in decolorization
Middle removal steam-stirring, steam blowing filter cake, it is ensured that the stability of bleached oil color manipulation, less decolorising agent usage amount change
It is apt to the odor contamination generated when blowing cake, reduces useless decolorising agent resid amount, improve bleaching workshop section yield, mitigates the decolorising agent that gives up to environment
Pollution problem；
Step 5: bleached oil is warming up to 240 DEG C, into deodorization plate tower, 230 DEG C of tower exit temperature, 40min is reacted, in steam
Pressure is pumped into deodorization filling material tower under conditions of being 0.06MPa, reacts 5min, deodorization filling material is discharged under 0.014MPa pressure at expulsion
Tower, tower exit temperature are cooled to 28 DEG C at 228 DEG C, through heat exchanger, are pumped into product oil stainless steel storage tank, are filled with 99.99% after tank is full
High pure nitrogen guarantees corn oil quality to reduce contact of the product oil with air to greatest extent.
Embryo is mentioned using wet process in the present embodiment, the crude oil that extract technology obtains, acid value AV 5.8mgKOH/g~
The product oil of 6.5mgKOH/g, acquisition are detected using national standard method, and as follows: index is shown in Table 1.
Embodiment 3
The refinery practice that corn oil quality is improved in the present embodiment, includes the following steps:
Step 1: balanced crude maize oil acid value: before refining of maize oil processing, crude maize oil being placed in crude maize oil storage tank
It is interior, use pressure for 6Kg/cm2Compressed air stir 5min, so that whole tank crude maize oil is in upper and lower level and seethe state, to reach
It is at equilibrium to lubricant component, acid value；
Step 2: alkali refining: the crude maize oil after balanced is pumped into crude oil processing tank through oil transfer pump, after filter filters, then
50 DEG C are heated to through heat exchanger, the food grade phosphoric acid of concentration 75% is added, the acid value after controlling acid adding, the value added of acid value is less than
0.15mgKOH/g reacts 30min, and the liquid alkaline of acid treated corn oil and 16 Baume degrees reacts 20min at 75 DEG C, through from
Heart equipment is separated, and obtained alkali refining oleic acid value is controlled in 0.15mgKOH/g hereinafter, saponified matter content≤200ppm, phosphorous≤
5ppm, zearalenone removal efficiency reach 38%；
Step 3: dewaxing: alkali refining oil is delivered in filter aid premixing tank after heat exchanger exchanges heat to 30 DEG C, pre- to filter aid
It mixes and the diatomite that oil weighs 3.5 ‰ is added in tank, after the completion of premix, the continuous crystallizing tank of temperature formula setting in gradient is pumped into, with 3
DEG C/h~4 DEG C/h speed cooling, temperature drop to 4 DEG C~6 DEG C after enter maturator keep the temperature 24 hours, oil temperature is then raised to 15
It DEG C is filtered, obtains dewaxed oil；
The generally existing filter aid additional amount of existing dewaxing technique is high, and oil loss is serious, and the dewaxing freezing experiment time is short to ask
Topic reduces filter aid dosage the invention can ensure that crystal grain straight uniform, improves oil yield, dewaxed oil freezing experiment up to 48h with
On；
Step 4: dewaxed oil enters decolorising agent premixing tank after heat exchanger exchanges heat to 110 DEG C, decolorising agent is added and mixes therewith
It closes, decolorising agent includes carclazyte and attapulgite, and the quality proportioning of carclazyte and attapulgite is 4:1, bleaching tower is pumped into after mixing, instead
Answer 100 DEG C of temperature, decolourize 20min, obtained bleached oil acid value in 0.18mgKOH/g~0.20mgKOH/g, color Y20,
R3.0, filtering, for vitamin E retention rate 89%, zearalenone removal efficiency reaches 32%, is 4Kg/cm in pressure2Pressure
Nitrogen blows cake 12min under the conditions of power, and the sump oil of filter cake blowout is pumped into bleaching tower through slop tank, sump oil color Y20, R3.0, filter cake
Residual oil 18%；
The existing generally existing decolorising agent dosage of decoloration process is big, and spent bleaching clay Residual oil is high, and bleached oil acid value increases higher, filter cake
Sump oil color out is deeper, it is more difficult to which the problem of increase of bleached oil color is caused after reuse or reuse, the present invention is in decolorization
Middle removal steam-stirring, steam blowing filter cake, it is ensured that the stability of bleached oil color manipulation, less decolorising agent usage amount change
It is apt to the odor contamination generated when blowing cake, reduces useless decolorising agent resid amount, improve bleaching workshop section yield, mitigates the decolorising agent that gives up to environment
Pollution problem；
Step 5: bleached oil is warming up to 240 DEG C, into deodorization plate tower, 230 DEG C of tower exit temperature, 40min is reacted, in steam
Pressure is pumped into deodorization filling material tower under conditions of being 0.06MPa, reacts 5min, deodorization filling material is discharged under 0.014MPa pressure at expulsion
Tower, tower exit temperature are cooled to 28 DEG C at 228 DEG C, through heat exchanger, are pumped into product oil stainless steel storage tank, are filled with 99.99% after tank is full
High pure nitrogen guarantees corn oil quality to reduce contact of the product oil with air to greatest extent.
Embryo is mentioned using semidry method in the present embodiment, the crude oil that squeezing process obtains, acid value AV 6.2mgKOH/g~
The product oil of 7.8mgKOH/g, acquisition are detected using national standard method, and as follows: index is shown in Table 1.
Embodiment 4
The refinery practice that corn oil quality is improved in the present embodiment, includes the following steps:
Step 1: balanced crude maize oil acid value: before refining of maize oil processing, crude maize oil being placed in crude maize oil storage tank
It is interior, use pressure for 6Kg/cm2Compressed air stir 5min so that whole tank crude maize oil is in upper and lower level and seethes state, with
It is at equilibrium to reach lubricant component, acid value；
Step 2: alkali refining: the crude maize oil after balanced is pumped into crude oil processing tank through oil transfer pump, after filter filters, then
60 DEG C are heated to through heat exchanger, the food grade phosphoric acid of concentration 75% is added, the acid value after controlling acid adding, the value added of acid value is less than
0.15mgKOH/g reacts 25min, and the liquid alkaline of acid treated corn oil and 12 Baume degrees reacts 20min at 80 DEG C, through from
Heart equipment is separated, and obtained alkali refining oleic acid value is controlled in 0.15mgKOH/g hereinafter, saponified matter content≤200ppm, phosphorous≤
5ppm, zearalenone removal efficiency reach 37%；
Step 3: dewaxing: alkali refining oil is delivered in filter aid premixing tank after heat exchanger exchanges heat to 30 DEG C, pre- to filter aid
It mixes and the diatomite that oil weighs 3.5 ‰ is added in tank, after the completion of premix, the continuous crystallizing tank of temperature formula setting in gradient is pumped into, with 3
DEG C/h~4 DEG C/h speed cooling, temperature drop to 4 DEG C~6 DEG C after enter maturator keep the temperature 24 hours, oil temperature is then raised to 14
It DEG C is filtered, obtains dewaxed oil；
The generally existing filter aid additional amount of existing dewaxing technique is high, and oil loss is serious, and the dewaxing freezing experiment time is short to ask
Topic reduces filter aid dosage the invention can ensure that crystal grain straight uniform, improves oil yield, dewaxed oil freezing experiment up to 48h with
On；
Step 4: dewaxed oil enters decolorising agent premixing tank after heat exchanger exchanges heat to 110 DEG C, decolorising agent is added and mixes therewith
It closes, decolorising agent includes carclazyte and attapulgite, and the quality proportioning of carclazyte and attapulgite is 3:1, bleaching tower is pumped into after mixing, instead
Answer 100 DEG C of temperature, decolourize 25min, obtained bleached oil acid value in 0.18mgKOH/g~0.20mgKOH/g, color Y20,
R2.9, for vitamin E retention rate 88%, zearalenone removal efficiency reaches 33%, and filtering is 4Kg/cm in pressure2Pressure
Nitrogen blows cake 12min under the conditions of power, and the sump oil of filter cake blowout is pumped into bleaching tower through slop tank, sump oil color Y20, R2.9, filter cake
Residual oil 18%；
The existing generally existing decolorising agent dosage of decoloration process is big, and spent bleaching clay Residual oil is high, and bleached oil acid value increases higher, filter cake
Sump oil color out is deeper, it is more difficult to which the problem of increase of bleached oil color is caused after reuse or reuse, the present invention is in decolorization
Middle removal steam-stirring, steam blowing filter cake, it is ensured that the stability of bleached oil color manipulation, less decolorising agent usage amount change
It is apt to the odor contamination generated when blowing cake, reduces useless decolorising agent resid amount, improve bleaching workshop section yield, mitigates the decolorising agent that gives up to environment
Pollution problem；
Step 5: bleached oil is warming up to 240 DEG C, into deodorization plate tower, 230 DEG C of tower exit temperature, 40min is reacted, in steam
Pressure is pumped into deodorization filling material tower under conditions of being 0.06MPa, reacts 5min, deodorization filling material is discharged under 0.012MPa pressure at expulsion
Tower, tower exit temperature are cooled to 28 DEG C at 228 DEG C, through heat exchanger, are pumped into product oil stainless steel storage tank, are filled with 99.99% after tank is full
High pure nitrogen guarantees corn oil quality to reduce contact of the product oil with air to greatest extent.
Embryo, the mixing crude oil that squeezing, extract technology obtain are mentioned using wet process and dry method in the present embodiment, acid value AV exists
The product oil of 8.0mgKOH/g~9.0mgKOH/g, acquisition are detected using national standard method, and as follows: index is shown in Table 1.
1 index table of table
Claims (1)
1. a kind of refinery practice for improving corn oil quality, which is characterized in that the technique specifically comprises the following steps:
1) balanced crude maize oil acid value: before refining of maize oil processing, crude maize oil is placed in crude maize oil storage tank, using pressure
For 6Kg/cm2Compressed air stir 5min, so that whole tank crude maize oil acid value is reached unanimity；
2) alkali refining: will be pumped into crude oil processing tank through oil transfer pump through step 1) treated crude maize oil, after filter filters, then
50 DEG C~60 DEG C are heated to through heat exchanger, the food grade phosphoric acid of concentration 70%~80% is added, the acid value after controlling acid adding, acid value
Value added be less than 0.15mgKOH/g, react 20min~30min, acid treated corn oil and 12 Baume degrees~16 Baume degrees
Liquid alkaline, 15min~20min is reacted at 70 DEG C~80 DEG C, is separated through centrifugation apparatus, the control of obtained alkali refining oleic acid value
In 0.15mgKOH/g hereinafter, saponified matter content≤200ppm, phosphorous≤5ppm, zearalenone removal efficiency reach 35% or more；
3) dewax: alkali refining oil is delivered in filter aid premixing tank after heat exchanger exchanges heat to 30 DEG C, is added into filter aid premixing tank
Enter the diatomite of oily weight 3 ‰~4 ‰, after the completion of premix, the continuous crystallizing tank of temperature formula setting in gradient is pumped into, with 3 DEG C/h~4
DEG C/cooling of the speed of h, temperature enters maturator after dropping to 4 DEG C~6 DEG C and keeps the temperature 24 hours, and oil temperature is then raised to 13 DEG C~15
It DEG C is filtered, obtains dewaxed oil；
4) decolourize, filter: dewaxed oil enters decolorising agent premixing tank after heat exchanger exchanges heat to 110 DEG C, and decolorising agent is added and mixes therewith
It closes, decolorising agent includes carclazyte and attapulgite, and the quality proportioning of carclazyte and attapulgite is (3~4): 1, decoloration is pumped into after mixing
Tower, 95 DEG C~105 DEG C of reaction temperature, decolourize 20min~30min, obtained bleached oil acid value 0.18mgKOH/g~
0.20mgKOH/g, color Y20, R2.9~3.1,88%~90%, zearalenone removal efficiency reaches vitamin E retention rate
To 30% or more, filtering is 4Kg/cm in pressure2Pressure condition under nitrogen blow cake 10min~15min, the dirt of filter cake blowout
Oil is pumped into bleaching tower through slop tank, sump oil color Y20, color Y20, R2.9~3.1, filter cake Residual oil≤18%；
5) be deodorized: bleached oil is warming up to 238 DEG C~240 DEG C, into deodorization plate tower, 230 DEG C of tower exit temperature, reacts 30min, is steaming
Steam pressure is pumped into deodorization filling material tower under conditions of being 0.04MPa~0.06MPa, 5min is reacted, in 0.012MPa~0.014MPa
Deodorization filling material tower is discharged under pressure at expulsion, tower exit temperature is cooled to 28 DEG C at 228 DEG C~230 DEG C, through heat exchanger, is pumped into product oil
Stainless steel storage tank, for vitamin E retention rate 75% or more, finished product oil index meets GB19111-2017 level-one oil standard,
120 DEG C, 8h returns color, color Y20, R2.9~3.2；105 DEG C of accelerated oxidation acid values are less than 0.1mgKOH/g, and α-VE a great deal of exists
25mg/100g~28mg/100g, content of trans fatty acids is less than 0.2%, and zearalenone content is in 25ppb hereinafter, sterol
Content is in 680mg/kg or more；
6) nitrogen charging: product oil is filled with nitrogen after entering product oil stainless steel storage tank, guarantees corn oil quality.
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| CN111534369A (en) * | 2020-04-29 | 2020-08-14 | 成都红旗油脂有限公司 | Preparation method of nutritional and healthy corn oil and corn oil prepared by preparation method |
| CN113186032A (en) * | 2021-05-31 | 2021-07-30 | 江南大学 | Method for decoloring peony seed oil |
| 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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| 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 |
| CN113916970A (en) * | 2021-08-31 | 2022-01-11 | 山东三星玉米产业科技有限公司 | Device and method for controlling heavy metal lead pollution risk in corn oil production |
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| CN115948198A (en) * | 2022-12-29 | 2023-04-11 | 长寿花食品股份有限公司 | Production process for controlling corn oil color reversion factor |
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| CN116200223B (en) * | 2023-01-05 | 2023-10-20 | 山东兴泉油脂有限公司 | Processing method of corn oil rich in phytosterol ester |
| CN116948744B (en) * | 2023-09-20 | 2023-12-08 | 曲阜良友食品有限公司 | Corn oil moderate processing technology |
| CN116948744A (en) * | 2023-09-20 | 2023-10-27 | 曲阜良友食品有限公司 | Corn oil moderate processing technology |
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