CN100513542C - Continuous oil fat refining process - Google Patents
Continuous oil fat refining process Download PDFInfo
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- CN100513542C CN100513542C CNB2006100452428A CN200610045242A CN100513542C CN 100513542 C CN100513542 C CN 100513542C CN B2006100452428 A CNB2006100452428 A CN B2006100452428A CN 200610045242 A CN200610045242 A CN 200610045242A CN 100513542 C CN100513542 C CN 100513542C
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Abstract
A continuous grease refinery process is carried out by felt oil-water debonding, acid refining, alkali refining, desoaping, washing and drying. It substitutes continuous acid refining reactor or/and continuous alkali refining reactor with alkali delay pot. It has homogeneous mix, proper contact time and full reaction.
Description
Technical field:
The invention belongs to the grease manufacture field, relate to the grease process for purification in the corn deep processing comprehensive utilization project, specifically a kind of production method and equipment of producing refined maize oil with maize germ.
Background technology:
China is large agricultural country, and agricultural resource is abundant, and the ultimate production of main farm produce, commodity amount are all at the forefront in the world, so deep processing of farm products is big rising industry.
Corn is one of main food crop of human plantation, accounts for 1/4th of world food overall crop yield.Corn also is the main food crop kind of China, and ultimate production is only second to paddy and wheat, occupies the second place of the world.The anxious especially economic field leaved for development of its comprehensive process.
The more direct effect of corn deep processing is the development of pulling agricultural industry chain, and corn resources development and use potentiality are very big, and its deep processing project is various, and is of many uses, and market capacity is big, the industry chain length, and development prospect is limitless.
Maize germ is the main byproduct of separating in the W-Gum course of processing.
The maize germ chemical constitution is:
Fat 46-55% protein 12-19% starch 8-12% ash content 0.7-1.2% fiber 15-18% other 2-3%
Semen Maydis oil is a kind of high-quality edible vegetable oil, and it contains 86% unsaturated fatty acids, and wherein 56% is linolic acid, and the human absorptivity can reach more than 97%; Containing saturated fatty acid is 14%.It contains abundant vitamin-E, and vitamin-E is a kind of natural antioxidants, needs the special vitamin-E that adds for anti-oxidation in a lot of oleaginous foods.Vitamin-E to human body cell division, certain effect has delayed senility.Content of vitamin E is only second to wheat germ oil in the crude oil of Semen Maydis oil, and it is heavy by 0.8%～1.2% still to contain oil after the deodorization.Sitosterol that contains and phosphatide have to prevent old and feeble effect, can reduce the content of cholesterol in human body, strengthen the function of human muscle and heart, vascular system, improve the resistivity of body.
The lipid acid of Semen Maydis oil is arranged therefore structural stablizing owing to be systematicness in sweet three esters; Simultaneously, general grease is under the effect of light, and chlorophyll can make its promote the oxidation, and does not have chlorophyll in the Semen Maydis oil, so Semen Maydis oil is more stable again.In view of above reason,, also there is the long quality guaranteed period than other oil even Semen Maydis oil also has suitable stability when the degree of depth is fried.
The Semen Maydis oil golden yellow color is transparent, and A sweety scent assails the nostrils, is well suited for cooking fast frying and frying oil, and it both can keep color and luster, the fragrance of vegetables and food, did not lose nutritive value again.
The Semen Maydis oil linoleic acid content is abundant, is the raw material of making medicines such as Maitong, linoleic acid on the medicine industry.
Start from the U.S. with the maize germ oil expression, trial production in 1890 puts goods on the market after 20 years in batches.Because its raw material is the byproduct of processing corn, aboundresources, favourable condition is many, develops into late 1970s, produces per year to have reached 200,000 tons.Also all there are certain industrial scale in some other in the world country such as Korea, Mexico, Saudi Arabia and Yugoslavia etc.
The maize germ resource of China is very abundant, and producing of Semen Maydis oil greatly developed in recent years, can open up new plant oil sources, obtain oil high-quality, that be of value to HUMAN HEALTH, can obtain albumen again, the development of pulling agricultural industry chain, its meaning is very long-range.
Semen Maydis oil is edible refined maize oil substantially in the world.Whole world Semen Maydis oil output, nineteen ninety is 1,490,000 tons, reaches 2,050,000 tons in 1999, average growth rate per annum is 3.6%.At present, China's corn consumption is about 1.2 hundred million tons, occupies the second place of the world, is only second to the U.S..Corn carry embryo oil expression the not enough corn total quantity consumed of ratio 4%.Development prospect is wide.
At present, produce Semen Maydis oil both at home and abroad and all adopt traditional grease production and method of refining, find no the pass and be specially adapted for the method for refining of Semen Maydis oil and the report of equipment.But the inventor finds after to the raw corn oil analysis, raw corn oil and other oil are planted very big difference, its feature is: maize germ is subjected to high temperature and treating with sulfurous acid in leaching process, so the raw corn oil peroxide value is higher, is generally about 3 (meq/kg); Acid value is also higher, is generally 5-6 (mgKOH/g); The p-anisidine value is very high, is generally 10; The color Vandyke brown.And natural oil plants such as soybean, peanut, cottonseed do not have high temperature and these situations for the treatment of with sulfurous acid.Also contain special wax and the higher 1-1.5% of being generally of phosphatide amount in the raw corn oil.Therefore, the fining process refined maize oil of applying mechanically soybean, cottonseed wet goods conventional oil fat does not reach high-quality requirement.
The phosphorus content of refining oil is the standard of refining effect.The refining oil quality good or not depends on the effect of acid, alkali refining.
Traditional oil refining process may further comprise the steps:
Crude oil-hydration degum-acid refining-alkali refining-take off soap-washing-drying.Then, through decolouring-dewaxing-deodorizing technology, obtain refining oil.
Acid refining is that the oil behind the hydration degum and a certain amount of phosphoric acid are added sour mixing tank simultaneously; Oil after the acid refining and a certain amount of caustic soda enter the alkali mixing tank simultaneously, reenter stirring-type time-delay jar neutralization reaction; Take off soap by supercentrifuge, finish the purpose of acid refining and alkali refining.
Think after analyses such as principle, structure, function and the using method research of inventor's process to former traditional stirring-type alkali refining time-delay jar: the alkali refining time-delay jar of former traditional technology, will there be 5.5KW (or bigger) electric motor the tank top as power, drive whipping appts by step-down gear, not stall in 24 hours is moving.Tank body is higher, and sealing and concentricity all are the problems of bad solution, often runs oil, leakage of oil, and the oil product of escape is excessive, and yield reduces.Main problem is that mixed solution causes mixed flow in the time-delay jar, the residence time is inaccurate, can not guarantee that the mixed solution that is introduced into the time-delay jar goes out earlier, make the material of part overstand take place aging, neutral oil increases, and too short material reaction of the residence time is incomplete, when particularly using this traditional process equipment refined maize oily, phosphorus content, soap content etc. does not reach the refining index.
Summary of the invention:
In order to make refinery practice meet the requirement of Semen Maydis oil characteristic more, further improve refined maize's oil quality, reduce refined maize's oil production cost and support equipment investment, improve the automation of operation level.The inventor has proposed to adopt acid, alkali refining flow reactor to implement the technical scheme of refining of maize oil.
Technical solutions according to the invention are a kind of processing method of continuous oil fat refining process, comprise crude oil hydration degum-acid refining-alkali refining-take off soap-technological processs such as washing-drying, it is characterized in that in acid, alkali boiling process, increase the acid refining flow reactor or/and the alkali refining flow reactor, substitute the alkali refining time-delay jar in the conventional grease refining process, be used to implement acid, the alkali boiling process of Semen Maydis oil.
The present invention provides acid, the design requirements of alkali flow reactor and processing parameter and the working method that adopts this reactor enforcement refining of maize oil simultaneously.
Acid of the present invention, alkali refining flow reactor are the cylindrical reactor of vertical installation, and two ends are taper, and its lower end is an opening for feed, and the upper end is a discharge port, are installed in respectively after acid, the alkali mixing tank, and opening for feed links to each other with acid, alkali mixer outlet respectively.
The feature technology parameter of acid of the present invention, alkali refining flow reactor be flow reactor length, the footpath than and mixture (mixed solution) residence time therein.
The length of flow reactor of the present invention, the footpath than, be key design parameter, it has determined flow state and the reaction effect of mixture in flow reactor.Through research of hydrokinetics mathematics model analysis and field application test, the inventor confirms, the length of acid refining flow reactor of the present invention, footpath are than being (2.5～5): 1, the length of alkali refining flow reactor, footpath are than being (6～9): 1 o'clock, and for implementing best design parameter scope of the present invention.
The residence time of material of flow reactor of the present invention is one of main technologic parameters, and through experimental study, the inventor confirms that acid refining flow reactor residence time of material is 0.7～1.2 minute, and alkali refining flow reactor residence time of material is 2～5 minutes.In this residence time scope, acid (or alkali) obtains thorough mixing and reaction uniformly with treating the refining crude oil, makes non-hydrophilic phosphatide (or neat soap) reach maximum cohesion, for the separation of next step whizzer provides reliable assurance.
The principle of work of acid of the present invention, alkali refining flow reactor is as follows: (is example with the alkali refining)
Crude oil material after hydration degum and acid refining is sent in the alkali mixing tank, with the alkali lye that enters simultaneously in the several seconds by shear powerful roughly mix after, send into from the bottom in the alkali refining flow reactor through piping again, further uniform mixing, and continue to finish the alkali refining reaction.The process of acid refining flow reactor is as the same.
In the alkali refining mixing tank with the mixed material fluid of alkali, laminar flow regime from small diameter pipeline, enter large diameter flow reactor, intermolecular distance rearranges turbulent flow takes place, and under the dynamic action of dehvery pump, the mixed oil liquid at about 1/3 place, flow reactor bottom forms stronger turbulence state, it is more even that mixed oil liquid is disperseed, molecular motion is violent, and speed of response is accelerated, and the free-fat acid-respons in alkali and the oil generates neat soap.During about 1/3～1/2 place, the flow state of mixed oil liquid relaxes gradually, forms stable laminar flow regime on flow reactor top, neat soap generate and growth process in, impurity such as absorption phosphatide, pigment, increase gradually.With the upper part, the flow state of mixed oil liquid relaxes more at flow reactor 1/2, and neat soap is attracted each other, the bigger neat soap that flocculates, and successively boost.Come the crunch of self-pumping that reliable kinetic energy is provided, make the mixed fluid that enters flow reactor form stable flowing, make the mixed oil liquid stable continuous enter and discharge.The state of the mutual back mixing of mixed oil liquid before and after no longer occurring.
If use instead from the flow reactor top and send into mixed oil liquid, liquid is come the dual function of self-pumping and feed liquid gravity, forms random motion, also produces mixed flow, does not reach processing requirement.
The design considerations of acid of the present invention, alkali refining flow reactor is as follows: (illustrating)
1. the mixing oil flow velocity that goes out 2 different cross sections by the fluid continuity equation inference has great difference: (Fig. 2)
When mixing oil enters the 2-2 cross section by the 1-1 cross section, because the fluid density in the two sections is constant, in the stationary state flow system, the flow through mass conservation in each cross section of fluid, and flow velocity U changes with pipeline section A:
U
1A
1＝U
2A
2
The sectional area A=∏/4d of garden pipe
2So following formula can be write as
U
1∏/4d
1 2＝U
2∏/4d
2 2
Get U thus
2/ U
1=(d
1/ d
2)
2
Work as d
1=50mm, d
2During=350mm
U
2/U
1＝(50/350)
2＝0.0204
Conclusion: cross section 2-2 speed is 2.04% of cross section 1-1 speed.Otherwise cross section 1-1 speed is 49 times of cross section 2-2 speed.Derive cross section 2-2 thus and have great difference than cross section 1-1 flow velocity.Characteristics with time expand.
2. the design considerations of the residence time:
I. establish the diameter d of cross section 1-1
1=50mm flow is Q
1=8 (m
3/ Hr) time,
8m
3/ Hr/60=0.133M
3/ minute,
By Q=UA, then
U
1=Q
1/ A
1=0.133/[3.14 (0.05/2)
2]=68M/ branch,
Q again
1=Q
2,
U
2=Q
2/ A
2=0.133/[3.14 (0.35/2)
2]=1.39M/ branch
A. the diameter d of working as cross section 2-2
2=350mm, when length was 1400mm, flow through time of this section of fluid was
1.4M/1.39M/ divide=1.01 (branches) to be used for the acid refining flow reactor
B. the diameter d of working as cross section 2-2
2=350mm, when length was 3000mm, flow through time of this section of fluid was
3M/1.39M/ divide=2.16 (branches) to be used for the alkali refining flow reactor
II. the diameter d of working as cross section 1-1
1=50mm, flow are Q
1=4 (m
3/ Hr) time
4 (m
3/ Hr)/60=0.0666M
3/ minute
U
1=Q
1/ A
1=0.0.0666/[3.14 (0.05/2)
2]=34M/ branch, in like manner
U
2=Q
2/ A
2=0.695M/ branch
A. the diameter d of working as cross section 2-2
2=170mm, when length was 700mm, flow through time of this section of fluid was
0.7M/0.695=1.01 (branch) is used for the acid refining flow reactor
B. the diameter d of working as cross section 2-2
2=170mm, when length was 1500mm, flow through time of this section of fluid was
1.5M/0.695M/ divide=2.16 (branches) to be used for the alkali refining flow reactor
According to the needs of process for refining or device fabrication installation, above-mentioned flow reactor not only can singly only use, and also can adopt two or two above serial or parallel connections uses.
The technical scheme that employing flow reactor of the present invention substitutes the alkali refining time-delay jar in the conventional grease refinery practice flow process is not only applicable to the refining of Semen Maydis oil, is applicable to that other is difficult to the extraordinary oil of purified yet.Use it for also can the be improved effect of quality product of common grease such as soybean oil, peanut oil.
Employing flow reactor of the present invention substitutes the technical scheme of the alkali refining time-delay jar in the conventional grease refinery practice flow process, oil mixes with acid, alkali, duration of contact is reasonable, sufficient reacting, the back mixing phenomenon of mixed fluid before and after having avoided, guarantee the mixed solution first outer, solved the not thorough and long problem of local reaction of purifying reaction, prevented the saponification of neutral oil effectively.Solved the processing method refined maize oil that uses traditional stirring-type alkali refining time-delay jar, quality product does not reach the problem of international edible oil common index.Use the method for the invention, acid value AV is stable, and saponified matter content is dropped to below the 80PPM by average 200PPM.Product quality indicator has reached the advanced index of international edible oil.
The refined maize's oil quality that adopts processing method of the present invention to reach is:
Project indicator operative norm
Smell, flavour: odorlessness, the good GB/T5525-1985 of mouthfeel
Transparency: clarification, transparent GB/T5525-1985
Color and luster (Lovibond cell 133.4mm) red 1.3 yellow 13 GB/T5525-1985
The GB/T5528 of moisture and volatile matter content/(%)≤0.05
The GB/T5529 of impurity/(%)≤0.05
(mg/g)≤0.10 GB/T5530 of acid number/(KOH)
Peroxide value/(mmol/kg) :≤1.5 GB/T5538
Smoke point/℃ 〉=215 GB/T17756-1999
Freezing test (0 ℃ of storage 30h): clarification, transparent GB/T17756-1999
Solvent residual amount/(mg/kg): do not detect GB/T5009.37
Refractive index (n
40): 1.456～1.468 GB/T5527
Relative density (d
20 20): 0.917～0.925 GB/T5526
Iodine number (I) is (g/100g): 107～135 GB/T5532
Adopt the inventive method in addition, do not need electric mixing device, 43560 degree can economize on electricity every year; After adopting the inventive method, do not need the complicated tightness system of former stirring time delay unit, exempted various maintenances; Oil, oil leakage phenomenon no longer take place to run, good stability, labor strength alleviates.Also can reduce 20,000 yuan of facility investments simultaneously.
Description of drawings:
Fig. 1 is the grease of the present invention process flow sheet of acid, alkali boiling method continuously
Fig. 2 is a material flow scaling system of the present invention
Embodiment:
Semen Maydis oil working method of the present invention, its technical process is:
Maize germ is through squeezing and to leach what obtain be raw corn oil; Raw corn oil is through hydration degum-acid refining-alkali refining-take off soap-washing-drying-decolouring-art breading such as dewaxing-deodorization to make the refined maize oil product.Hydration degum--acid refining-alkali refining-Tuo soap-washing-drying process is seen accompanying drawing 1
Raw corn oil enters crude oil jar 1, be heated to 75 ℃ with pump 2 by plate-type heat exchanger 3,4, after in static mixer 5, mixing, adding hot soft water in aquation oil tank 6 stirs, send into disc centrifuge 8 with pump 7, oil behind the hydration degum enters oil tank 9, be heated to 85-90 ℃ by pump 10 at plate-type heat exchanger 11, adding concentration at sour mixing tank 12 is 85% phosphoric acid, add-on is the 0.15%---0.2% of crude oil amount, enter time-delay reaction in the sour flow reactor 13 behind sour mixing tank thorough mixing, be 0.94-1.1 minute duration of contact.And then enter to enter in the alkali flow reactor 15 behind another alkali mixing tank 14 thorough mixing and fully contact fast and reposefully with alkali, be 2-5 minute every duration of contact.Alkali lye (NaOH) concentration is 18--20Be ', and alkali charge is the 118--122% of theoretical alkali.Material behind acid, the alkali refining is sent into and is taken off soap disc centrifuge 16, and soap is entered in 26 jars with pumping out.Material is by pump 17 after taking off soap, send into plate-type heat exchanger 18 and the softening water of pump 19 from hot-water cylinder, enter together that water mixer 20 is laggard goes into to wash disc centrifuge, before plate-type heat exchanger 18, add an amount of citric acid, be residual soap flocculation, enter at last and dehydrate, send into next procedure with pump 23.
24, the 25,26,27,28, the 29th, colloid, soap stock remover.
Embodiment 1.
Day is handled the production line of 200 tons of raw corn oils
1 of acid flow reactor: diameter 350MM, long 1400MM (two ends are cone).
Material is 1.01 minutes residence time in flow reactor
Alkali flow reactor diameter 350MM, long 3000MM (two ends are cone).2 polyphones.Material is 4.32 minutes residence time in flow reactor
Former known soybean oil refinery practice has only stirring-type alkali time-delay jar.The present invention increases 1 of sour flow reactor newly, and increases by 2 replacements of alkali flow reactor stirring-type alkali time-delay jar.
This cover reactor reaches processing requirement fully.
The quality product of itself and traditional technology is compared as follows:
The FFA% that comes unstuck, the present invention can reach 0.05%, and traditional technology is generally 0.5%, improves 10 times.
Soap content, the present invention can reach 20PPM, and traditional technology is generally 150PPM, improves 7.5 times.
Day is handled the production line of 1000 tons of raw corn oils
Flow reactor amplifies by same ratio, all can reach These parameters.
That is: the diameter d of cross section 1-1
1=100mm, d
2=600mm, flow are Q
1=42 (m
3/ Hr) time, 42m
3/ Hr/60=0.7M
3/ minute,
By Q=UA, then
U
1=Q
1/ A
1=0.7/[3.14 (0.1/2)
2]=89.2M/ branch,
Q again
1=Q
2,
U
2=Q
2/ A
2=0.7/[3.14 (0.6/2)
2]=2.48M/ branch
A. the diameter d of working as cross section 2-2
2=600mm, when length was 2800mm, flow through time of this section of fluid was
2.8M/2.48M/ divide=1.129 (branches) to be used for the acid refining flow reactor
B. the diameter d of working as cross section 2-2
2=600mm, when length was 5000mm, flow through time of this section of fluid was
5M/2.48M/ divide=2.02 (branches) to be used for the alkali refining flow reactor.2 polyphones.Material is 4.04 minutes residence time in flow reactor.
This cover reactor reaches processing requirement fully.
The product quality of itself and traditional handicraft is compared as follows:
The FFA% that comes unstuck, the present invention can reach 0.05%, and traditional handicraft is generally 0.5%, improves 10 times.
Soap content, the present invention can reach 20PPM, and traditional handicraft is generally 150PPM, improves 7.5 times.
Claims (3)
1. the grease processing method of acid, alkali boiling continuously, comprise crude oil hydration degum-acid refining-alkali refining-Tuo soap-washing-drying process, it is characterized in that in acid, alkali boiling process, increase acid refining flow reactor and alkali refining flow reactor, substitute the alkali refining time-delay jar in the conventional grease refining process, be used to implement acid, the alkali boiling process of Semen Maydis oil; Said acid, alkali flow reactor are the cylindrical reactor of vertical installation, and two ends are taper, and its lower end is an opening for feed, and the upper end is a discharge port, are installed in respectively after acid, the alkali mixing tank, and opening for feed links to each other with acid, alkali mixer outlet respectively; The length of above-mentioned acid refining flow reactor, footpath are than being (2.5～5): 1, and the length of alkali refining flow reactor, footpath are than being (6～9): 1.
2. grease as claimed in claim 1 is the processing method of acid, alkali boiling continuously, it is characterized in that the residence time of material in the acid refining flow reactor is 0.7～1.2 minute; The residence time of material in the alkali refining flow reactor is 2～5 minutes.
3. grease as claimed in claim 1 is the processing method of acid, alkali boiling continuously, it is characterized in that processing step and operational condition are as follows:
Raw corn oil enters crude oil jar 1, pass through plate-type heat exchanger 3 with pump 2,4 are heated to 75 ℃, after in static mixer 5, mixing, adding hot soft water in aquation oil tank 6 stirs, send into disc centrifuge 8 with pump 7, oil behind the hydration degum enters oil tank 9, be heated to 85～90 ℃ by pump 10 at plate-type heat exchanger 11, adding concentration at sour mixing tank 12 is 85% phosphoric acid, add-on is 0.15～0.2% of a crude oil amount, behind sour mixing tank thorough mixing, enters time-delay reaction in the sour flow reactor 13, be 0.94～1.1 minute duration of contact, and then enter another alkali mixing tank 14, and entering behind the thorough mixing in the alkali flow reactor 15 and fully contact fast and reposefully with alkali, be 2～5 minutes duration of contact, the NaOH concentration of lye is 12.59～14.24%, and alkali charge is 118～122% of a theoretical alkali; Material behind acid, the alkali alkali refining is sent into and is taken off soap disc centrifuge 16, soap is entered in 26 jars with pumping out, material is by pump 17 after taking off soap, send into plate-type heat exchanger 18, adding an amount of citric acid before plate-type heat exchanger 18, is residual soap flocculation and pump 19 softening water from hot-water cylinder, enters together that water mixer 20 is laggard goes into to wash disc centrifuge 21, enter at last and dehydrate, send into next procedure with pump 23.
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|---|---|---|---|
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| CN102140386B (en) * | 2011-01-24 | 2012-10-24 | 青岛福瑞斯生物能源科技开发有限公司 | Method for degumming biodiesel |
| CN102250683B (en) * | 2011-06-15 | 2013-03-20 | 晨光生物科技集团股份有限公司 | Alkali refining process of cottonseed oil |
| CN102228093B (en) * | 2011-06-29 | 2013-03-27 | 山东西王食品有限公司 | Maize germ oil production process with six fresh-keeping steps |
| CN103205311B (en) * | 2013-05-06 | 2014-12-24 | 国家粮食局科学研究院 | Method for industrially removing zearalenone out of maize germ |
| CN103952228A (en) * | 2014-04-29 | 2014-07-30 | 陶建壮 | Process of extracting maize embryo oil |
| CN117305016A (en) * | 2023-10-19 | 2023-12-29 | 湖南师范大学 | Refined oil neutralization process optimization control method based on intelligent decision-making mode mining |
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