CN102533441A - Degumming process for edible vegetable oil and application thereof - Google Patents
Degumming process for edible vegetable oil and application thereof Download PDFInfo
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- CN102533441A CN102533441A CN2012100199497A CN201210019949A CN102533441A CN 102533441 A CN102533441 A CN 102533441A CN 2012100199497 A CN2012100199497 A CN 2012100199497A CN 201210019949 A CN201210019949 A CN 201210019949A CN 102533441 A CN102533441 A CN 102533441A
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Abstract
The invention relates to a degumming process for edible vegetable oil and the application thereof. The degumming process for edible vegetable oil comprises the following steps: reacting raw oil with an acid to convert non-hydrated phospholipids in the raw oil into hydrated phospholipids, agglomerating micelles by hydration, and performing centrifugal separation to obtain degummed oil. The degumming process for edible vegetable oil can be applied to refining of edible vegetable oil. The invention further discloses a process of refining edible vegetable oil, which can produce RBD oil products by performing the following steps in sequence: degumming process mentioned above, decoloring treatment, deacidifying treatment and deodorizing treatment. The degumming process for edible vegetable oil is suitable for degumming of various edible vegetable oil, particularly seed oil with high phosphorus content (more particularly seed oil with high non-hydrated phospholipids content), and has excellent degumming effect. The degumming process is an innovation in oil and fat degumming aspect, and besides, the improvement on the degumming process promotes the generation of novel physical refining techniques in oil processing.
Description
Technical field
The present invention relates to the edible oil manufacture field, be specifically related to the degumming technology and the application thereof of edible vegetable oil.
Background technology
The production of all edible vegetable oils all will be through degumming raw oil, take off refining procedure processing such as assorted, depickling, precipitation, drying, decolouring, deodorization and winterization dewaxing comes; Because the difference of crude oil kind and processed oil class requirement; The procedure technology of the course of processing maybe be slightly different; Yet no matter the kind index of crude oil and processed oil class requirement why not have with, the workshop section of wherein coming unstuck all is absolutely necessary in each technology.
The degumming technology that current line exists in the industry comprises that water comes unstuck, special coming unstuck and enzymatic degumming.Wherein, the water defective of coming unstuck is to remove nonhydratable phosphatide; It is not thorough that special defective of coming unstuck is that phosphatide removes, and phosphorus content is greater than 20ppm; The removal effect of enzymatic degumming is good, but defective is the on the high side of enzyme, and production cost is high relatively.
The direct or indirect technological effect that influences other workshop section of quality meeting of degumming technology effect.If the effect of its workshop section of coming unstuck merely of oil and fat refining production line is undesirable; Just must through in reach degumming effect comparatively completely with depickling or through the auxiliary degumming effect that atlapulgite is added in decolouring; Yet this unavoidable auxiliary degumming processing certainly will reduce the product yield; Increase the consumption of supplementary material and neutral oil, but also can increase the possibility of sewage discharge.
The edible vegetable oil physical refining process only is to be used in the low palmitic processing of gel content at present.For the high seed oil of the especially nonhydratable phospholipids content of rapeseed oil soybean wet goods phosphorus content height, owing to there is not the degumming technology of economic and reliable, large industrialized production all will be adopted the chemical refining operation basically in order to reach necessary degumming effect.
Summary of the invention
The object of the invention overcomes defective of the prior art exactly, and a kind of degumming technology and application thereof of edible vegetable oil are provided.
The present invention at first discloses a kind of degumming technology of edible vegetable oil, for elder generation is converted into hydrated phospholipid with crude oil and acid-respons with the nonhydratable phosphatide in the crude oil, and after aquation cohesion micelle obtains degummed oil through spinning again.
Concrete, said degumming technology comprises the following steps:
1) transforms: be that 50--70 ℃ crude oil is with after the Hydrocerol A that accounts for crude oil weight 0.05-0.5%, phosphoric acid, oxysuccinic acid or oxalic acid mix with temperature; In the acid-respons jar stirring reaction 15-30 minute; Accomplish the reaction that nonhydratable phosphatide is converted into hydrated phospholipid, obtain transformation mixture;
2) aquation: after transformation mixture and the 20-50 ℃ of weight 1.5-2.5 soft water doubly that is phosphatide weight in the crude oil mixed, temperature adjustment was to 20-45 ℃, and in the hydration reaction jar stirring reaction 45-150 minute, the completion hydration reaction obtained hydrated mixt;
3) spinning: hydrated mixt is heated to 75-90 ℃ after the whizzer spinning, separates the thing that gently is separated that obtains and after vacuum precipitation drying, obtain degummed oil.
More specifically:
In the step 1),
Said crude oil can be the crude oil of any edible vegetable oil, includes but not limited to: Crude Dapeseed Oil, green soy bean oil, sunflower seeds crude oil, maize germ crude oil, hair Rice pollard oil (also claiming hair rice oil).
Preferable, the phosphorus content of said crude oil is 100-700ppm (mg/kg), impurity content＜0.2wt%.
Crude oil can adopt board-like or tubular heat exchange or heater heats to 50--70 ℃.
Used acid can be selected from Hydrocerol A, phosphoric acid, oxysuccinic acid, oxalic acid.Preferable, Hydrocerol A, phosphoric acid, oxysuccinic acid or oxalic acid account for crude oil weight 0.15-0.5%.
Cited like the embodiment of the invention, after acid can be disposed aqueous acid earlier, add in proportion.The aqueous citric acid solution that for example adds 50wt%.
The stirring velocity of stirring reaction generally is controlled to be 45-60 rev/min in the said acid-respons jar.
Through step 1), in the crude oil, nonhydratable phosphatide is converted into reactivity＞99.5% of hydrated phospholipid.
Step 2) in,
Said soft water is for being lower than the soft water of 10 degree (German degree).
Said transformation mixture can adopt plate-type heat exchanger cooling temperature adjustment with after said soft water mixes.
The stirring velocity of stirring reaction generally is controlled to be 35-75 rev/min in the said hydration reaction jar, and the hydration reaction residence time can be 45-150 minute, generally is controlled to be 45-120 minute.The stirring velocity and the reaction times of hydration reaction are adjustable, can be according to crude oil kind phosphorus content and temperature of reaction adjustment.Generally speaking, the crude oil phosphorus content is high or temperature of reaction is high, but agitation as appropriate hurry up, and the temperature of reaction low reaction time is long.
In the step 3),
Said mixture through aquation can be through board-like or tubular heat exchange or heater heats to 75-90 ℃.
Preferable, through the first mixture heat exchange of the mixture of aquation, being heated to 75-90 ℃ through board-like or tubular heat exchange again through plate-type heat exchanger and water inletization retort, this design can be further energy-conservation.
The said thing that gently is separated can be first gently the be separated thing or separate second thing that gently is separated that obtains through the whizzer two times centrifugal that obtains through a spinning of whizzer.
Saidly be specially: hydrated mixt is heated to 75-90 ℃ after the first whizzer spinning obtains first thing that gently is separated through the isolating method of whizzer two times centrifugal; Said first gently the be separated soft water of thing weight 2.5-5% of thing and 75-90 ℃ account for said first that gently is separated is mixed; Oil-water mixture got into the washing of washing remaining tank after 10-30 minute; Again through the second whizzer spinning, obtain second thing that gently is separated.Big at the crude oil impurity content, the crude oil phospholipids content is higher relatively, to the degummed oil phosphorus content require not high relatively and the not enough situation of separate unit whizzer separating power under, can adopt two times centrifugal to separate.Under only production level Four degummed oil and the competent situation of one bench centrifuge separating power, only need a spinning.
During said two times centrifugal is separated, when oil-water mixture gets into the washing of washing remaining tank, can follow stirring simultaneously, stirring velocity can soon can be slow, general controlledly is made as 0-60 rev/min.Said soft water is for being lower than the soft water of 10 degree (German degree).
The used whizzer of spinning can adopt disk plate centrifuge.
Preferable, in order to exempt the processing of heavy phase isolate (being waste water) after the spinning, can with through the heavy phase isolate of the second whizzer spinning as step 2) in the soft water source.But the not only water saving of this step also can reduce the processing and the discharging of waste water.
Further, before the thing vacuum that gently the is separated precipitation drying, be heated to 75-120 ℃, be preferably 85-115 ℃.This step can adopt board-like or tubular heat exchange or heater heats.If without heating, the thing that gently is separated has reached temperature requirement (more than 75 ℃), and then this step can be omitted.
Preferable, the residual voltage when said vacuum precipitation is dry is 25-100mpa.Can be dried to moisture content＜0.1wt%.Precipitation to residual dissolving reduced to＜30ppm.
Vacuum precipitation drying can adopt vacuum drier to carry out, like spraying drying type or baffle plate overflow type vacuum drier.
Degumming method of the present invention is changed nonhydratable phosphatide through acid-respons; Rehydration cohesion micelle; Separate (conversion-aquation-spinning) through whizzer, it is qualified that the degummed oil phosphorus content of acquisition can reach 280 ℃ of heating experiments of GB, the phosphorus content index＜10ppm of degummed oil; Needn't pass through chemical refining in workshop section and directly get into decoloration and deodorization workshop section, can adopt the operational path production one-level oil of physical refining fully.
The degumming technology of edible vegetable oil of the present invention can be used for the refining of edible vegetable oil.
The present invention also further discloses a kind of edible vegetable oil refinery practice, comprises the following steps:
A. crude oil is adopted earlier the degumming technology according to the invention acquisition degummed oil that comes unstuck;
B. degummed oil without in directly decolour with depickling and to obtain decolouring edible vegetable oil;
C. decolour edible vegetable oil behind deacid-deodoring, obtain finished product RBD oil (refining decoloration and deodorization oil) through cooling and smart filter.
Concrete,
In the step a),
Said degummed oil phosphorus content＜10ppm, moisture content＜0.1wt%.
If degummed oil moisture content >=0.1wt%, then step a) increases drying step, makes degummed oil moisture content＜0.1wt%.
In the step b),
Said decolouring can be adopted decoloration process one time, also can adopt secondary decolourization technology (also claiming to take off in advance to take off technology again) for reducing carclazyte consumption.
Preferable; The method that said decolouring obtains decolouring edible vegetable oil is specially: said degummed oil is heated to 105-120 ℃; Under the 50-150mbar absolute pressure, add the atlapulgite that accounts for said degummed oil weight 0.5-2.0%; Behind 25-45 minute decoloring reaction, obtain decolouring edible vegetable oil through filtering successively with smart filter.
Degummed oil can adopt board-like or tubular heat exchange or heater heats to 105-120 ℃.
Filtration can be adopted filter, and smart filter can be adopted the insurance strainer.
In the step c),
Preferable, during deacid-deodoring, stripping gas adds the 0.3-1.5% of weight for decolouring edible vegetable oil weight, is more preferred from 0.3-1.0%.
Concrete, the method for said decolouring edible vegetable oil deacid-deodoring can be selected from following arbitrary:
After I, the edible vegetable oil that will decolour are heated to 240-260 ℃, through the deacid-deodoring tower deacid-deodoring;
After II, the edible vegetable oil that will decolour are heated to 240-260 ℃, earlier through the extracting tower depickling, again through the deodorization of deodorization tower;
After III, the edible vegetable oil that will decolour are heated to 240-260 ℃, earlier through the deodorization of deodorization tower, again through the extracting tower depickling;
Preferable, method I) in, the structured packing tower structure is partly adopted in the depickling of said deacid-deodoring tower, and the tray column structure is partly adopted in deodorization.The packing tower of said deacid-deodoring tower can be formerly, in the back or in the centre.
Preferable, advance the tower deacid-deodoring before, decolouring edible vegetable oil FFA (free fatty acids) content is 0.05wt%--4wt%; Absolute pressure＜2.5mbar when depickling and deodorization; Deacid-deodoring total time is 45min--120min (wherein, the depickling time is shorter, generally is no more than 5min).
Preferable, the heating means of decolouring edible vegetable oil are: will decolour edible vegetable oil at first with the high temperature oil heat exchange that goes out tower through deacid-deodoring, pass through HP steam or other thermal source again and be heated to 240-260 ℃.This measure can be further energy-conservation.
Edible vegetable oil refinery practice of the present invention successively through come unstuck, decolouring, deacid-deodoring (distillation method disacidify) obtain the RBD processed oil, whole process does not have in the independent alkali refining and the depickling step, is physical refining.
Beneficial effect of the present invention:
Edible vegetable oil degumming technology of the present invention is applicable to any plant oil degumming; Especially for the high seed oil of the especially nonhydratable phospholipids content of phosphorus content height; The good characteristics of degumming effect are more outstanding; This singly is not the innovation aspect fat degumming, and the progress of this kind degumming technology has driven and produces novel grease processing physics refining techniques.
Edible vegetable oil refinery practice of the present invention is abandoned chemical refining and is adopted the advantage of physical refining to be:
The yield that 1) can improve processed oil is made an appointment with (rapeseed oil improves yield 0.8%--1%, VT 18 improves yield 0.6%--0.8%);
2) there has not been the discharging (usually about 6% of the chemical refining washing sewage flow rate amount of accounting for) of neutralization washing water waste water;
3) adopt physical refining not have the processing costs of phosphorous soap stock; The output and quality (the about rapeseed oil 1% of lipid acid output raising of the acid of high value sub product deodorised fat have been improved; Soya-bean oil 0.8%; The FFA of lipid acid is increased to 75% by 50% content), auxiliary materials such as other carclazyte use suitable with chemical refining.
Embodiment
Below enumerate specific embodiment with further elaboration the present invention, should be understood that instance is not to be used to limit protection scope of the present invention.
Embodiment 1
Raw material: Canadian Kano is drawn and is leached Crude Dapeseed Oil one of (nonhydratable phospholipids content be in the vegetables oil the highest), acid value 1.8mgKOH/g, phosphorus content 650ppm.
Adopt following technology to come unstuck:
Normal temperature leaches the board-like or tubular heat exchange (well heater) of Crude Dapeseed Oil (containing assorted＜0.2%) and is heated to 65 ℃; It is the 50wt% aqueous citric acid solution that cutter formula or centrifugal mixer add concentration; Account for crude oil weight 0.28% until Hydrocerol A, get into the retort of belt stirrer, stirring velocity 45-60 rev/min; In 30 minutes reaction times, the nonhydratable phosphatide in reaction back is converted into reactivity＞99.5% of hydrated phospholipid; Add normal-temperature water (20-50 ℃), amount of water is the soft water of 2 times of phosphatide weight contents, add after the water through plate-type heat exchanger heat exchange cooling, the oil temperature 35 ℃ water--oil gets into the hydration reaction jar.35-75 rev/min of hydration reaction jar belt stirrer rotating speed, 90 minutes hydration reaction residence time.Through the hydration reaction jar; Reaction mixture is through the mixture heat exchange of plate-type heat exchanger with the water inletization retort; Be heated to 85 ℃ through board-like or tubular heat exchange again; Obtain the soft water (soft water temperature 85 ℃) of light phase degummed oil through cutter formula or centrifugal mixer adding degummed oil weight 2.5% through the disk plate centrifuge separation, oil-water gets into washing remaining tank, 25 minutes residence time; Get into second bench centrifuge through washing oil pump oil-water mixture then; Gently be separated thing degumming water washing oil again (oil temperature low words be heated to 88 ℃) through tubulation or plate heater get into precipitation moisture eliminator, the precipitation moisture eliminator is worked under the 25-100mpa residual voltage, goes out the precipitation moisture eliminator and promptly gets degummed oil.
Detect: degummed oil phosphorus content 8ppm, 280 ℃ of heating experiment nothings are separated out the residual molten 22ppm of degummed oil, degummed oil FFA content 0.85%.
Embodiment 2
Raw material: Canadian Kano plucking rapeseed oil, acid value 1.8mgKOH/g, phosphorus content 650ppm.
Adopt following technology to come unstuck:
The normal temperature Crude Dapeseed Oil (contains assorted＜0.2%; FFA content 0.9%) board-like or tubular heat exchange (well heater) is heated to 65 ℃, and it is the 50wt% aqueous citric acid solution that cutter formula or centrifugal mixer add concentration, accounts for crude oil weight 0.28% until Hydrocerol A; Get into the retort of belt stirrer; Stirring velocity 45-60 rev/min, in 30 minutes reaction times, the nonhydratable phosphatide in reaction back is converted into reactivity＞99.5% of hydrated phospholipid; Add normal-temperature water (20-50 ℃), amount of water is the soft water of 2 times of phosphatide weight contents, add after the water through plate-type heat exchanger heat exchange cooling, the oil temperature 35 ℃ water--oil gets into the hydration reaction jar.35-75 rev/min of hydration reaction jar belt stirrer rotating speed, 90 minutes hydration reaction residence time.Through the hydration reaction jar; Reaction mixture is through the mixture heat exchange of plate-type heat exchanger with the water inletization retort; Be heated to 85 ℃ through board-like or tubular heat exchange again; Obtain light phase degummed oil (the low words of oil temperature are heated to 85 ℃ through tubulation or plate heater) through the disk plate centrifuge separation and get into the precipitation moisture eliminator, the precipitation moisture eliminator is worked under the 25-100mpa residual voltage, goes out the precipitation moisture eliminator and promptly gets degummed oil.
Detect: degummed oil phosphorus content 15ppm, 280 ℃ of heating experiment nothings are separated out the residual molten 26ppm of degummed oil, degummed oil FFA content 0.85%.
Embodiment 3
Raw material: hair Fructus Maydis oil, acid value 1.0mgKOH/g, phosphorus content 300ppm.
Adopt following technology to come unstuck:
Board-like or the tubular heat exchange (well heater) of normal temperature hair Fructus Maydis oil (containing assorted＜0.2%) is heated to 50 ℃; It is the 50wt% aqueous citric acid solution that cutter formula or centrifugal mixer add concentration; Account for crude oil weight 0.15% until Hydrocerol A, get into the retort of belt stirrer, stirring velocity 45-60 rev/min; In 15 minutes reaction times, the nonhydratable phosphatide in reaction back is converted into reactivity＞99.5% of hydrated phospholipid; Add normal-temperature water (20-50 ℃), amount of water is the soft water of 1.5 times of phosphatide weight contents, add after the water through plate-type heat exchanger heat exchange cooling, the oil temperature 20 ℃ water--oil gets into the hydration reaction jar.35-75 rev/min of hydration reaction jar belt stirrer rotating speed, 45 minutes hydration reaction residence time.Through the hydration reaction jar; Reaction mixture is through the mixture heat exchange of plate-type heat exchanger with the water inletization retort; Be heated to 75 ℃ through board-like or tubular heat exchange again, separate obtaining the soft water (soft water temperature 75 ℃) of light phase degummed oil through cutter formula or centrifugal mixer adding degummed oil weight 2.5-5% through disk plate centrifuge, oil-water gets into the washing remaining tank; 60 rev/mins of water washing tank stirring velocitys; 10 minutes time got into second bench centrifuge through washing oil pump oil-water mixture then, and thing degumming water washing oil (the low words of oil temperature are heated to 110 ℃ through tubulation or plate heater) entering precipitation moisture eliminator gentlier is separated; The precipitation moisture eliminator is worked under the 100mpa residual voltage, goes out the precipitation moisture eliminator and promptly gets degummed oil.
Detect: degummed oil phosphorus content 9ppm, 280 ℃ of heating experiment nothings are separated out the residual molten 28ppm of degummed oil, degummed oil FFA content 0.5%.
Embodiment 4
Raw material: hair leaches Crude Dapeseed Oil, acid value 2.0mgKOH/g, phosphorus content 700ppm.
Adopt following technology to come unstuck:
The normal temperature hair leaches the board-like or tubular heat exchange (well heater) of Crude Dapeseed Oil (containing assorted＜0.2%) and is heated to 70 ℃; It is the 50wt% aqueous citric acid solution that cutter formula or centrifugal mixer add concentration; Account for crude oil weight 0.5% until Hydrocerol A, get into the retort of belt stirrer, stirring velocity 45-60 rev/min; In 25 minutes reaction times, the nonhydratable phosphatide in reaction back is converted into reactivity＞99.5% of hydrated phospholipid; Add normal-temperature water (20-50 ℃), amount of water is the soft water of 2.5 times of phosphatide weight contents, add after the water through plate-type heat exchanger heat exchange cooling, the oil temperature 45 ℃ water--oil gets into the hydration reaction jar.35-75 rev/min of hydration reaction jar belt stirrer rotating speed, 120 minutes hydration reaction residence time.Through the hydration reaction jar; Reaction mixture is heated to 90 ℃ through board-like or tubular heat exchange again through the mixture heat exchange of plate-type heat exchanger with the water inletization retort, separates obtaining light phase degummed oil adds degummed oil weight 2.5-5% through cutter formula or centrifugal mixer soft water (90 ℃ of soft water temperature) through disk plate centrifuge; Oil-water gets into the washing remaining tank; 30 minutes time got into second bench centrifuge through washing oil pump oil-water mixture then, and thing degumming water washing oil (the low words of oil temperature are heated to 88 ℃ through tubulation or plate heater) entering precipitation moisture eliminator gentlier is separated; The precipitation moisture eliminator is worked under the 25mpa residual voltage, goes out the precipitation moisture eliminator and promptly gets degummed oil.
Detect: degummed oil phosphorus content 6ppm, 280 ℃ of heating experiment nothings are separated out the residual molten 22ppm of degummed oil, degummed oil FFA content 0.45%.
Embodiment 5
Raw material: Canadian Kano plucking rapeseed oil, acid value 1.8mgKOH/g, phosphorus content 650ppm contains assorted 0.1%.
Adopt following refinery practice refining:
Adopt the Degumming Procedures of embodiment 1 to prepare degummed oil (moisture＜0.1%), adopts board-like or tubular heat exchange adjustment temperature to 110 ℃, adding accounts for degummed oil weight 1% atlapulgite under the 100mbar absolute pressure; Through the decoloring reaction of 35min, get into filter and filter, the edible vegetable oil that comes out is again through the smart filter of insurance strainer; Decolouring edible vegetable oil gets into deacid-deodoring workshop section (stripping gas addition; Oil is heavy by 0.8%), decolouring edible vegetable oil at first with the processed oil heat exchange of coming out of deodorization tower, be heated to 258 ℃ through HP steam or other thermal source again; Get into deacid-deodoring tower; The decolouring edible vegetable oil FFA content that gets into deacid-deodoring tower is at 1.2wt%, the absolute pressure 2.2mbar of deacid-deodoring, and deodorization time is at 90min; Deacid-deodoring oil that comes out and the energy-conservation heat exchange of decolouring edible vegetable oil of advancing tower promptly obtain finished product RBD oil (final decoloration and deodorization processed oil) through last interchanger cooling and secondary filter again.
Detect: adopt (the acid number check: press GB/T 5530 execution and detect of relevant GB standard detection; Heat test: press GB/T 5531 and carry out; Moisture and volatile matter content check: press GB/T 5528 and carry out) Colour Measurement: the 2nd chapter of pressing among the GB/T 5525-1985 is carried out; Smoke point check: press GB/T 177561999 appendix B and carry out), processed oil FFA content is 0.035%, processed oil color and luster R1.1Y12; 218 ℃ of processed oil smoke points, calculating the processed oil yield with processed oil yield=processed oil quality/quality of crude oil is 95.1%.
Embodiment 6
Raw material: Canadian Kano is drawn and is leached Crude Dapeseed Oil (nonhydratable phospholipids content be in the vegetables oil), acid value 1.8mgKOH/g, phosphorus content 650ppm.
Adopt following refinery practice refining:
Adopt the Degumming Procedures of embodiment 1 to prepare degummed oil (moisture＜0.1%), adopts board-like or tubular heat exchange adjustment temperature to 105 ℃, adding accounts for degummed oil weight 2.0% atlapulgite under the 50mbar absolute pressure; Through the decoloring reaction of 45min, get into filter and filter, the edible vegetable oil that comes out is again through the smart filter of insurance strainer; Decolouring edible vegetable oil gets into deacid-deodoring workshop section (stripping gas addition; Oil is heavy by 0.3%), decolouring edible vegetable oil at first with the processed oil heat exchange of coming out of deodorization tower, be heated to 240 ℃ through HP steam or other thermal source again; Get into deacid-deodoring tower; The decolouring edible vegetable oil FFA content that gets into deacid-deodoring tower is at 1.2wt%, the absolute pressure＜2.5mbar of deacid-deodoring, and deodorization time is at 45min; Deacid-deodoring oil that comes out and the energy-conservation heat exchange of decolouring edible vegetable oil of advancing tower promptly obtain finished product RBD oil (final decoloration and deodorization processed oil) through last interchanger cooling and secondary filter again.
Detect: processed oil FFA content is 0.045%, processed oil color and luster Y10R0.8, and 216 ℃ of processed oil smoke points, the processed oil yield is 95.45%.
Embodiment 7
Raw material: Canadian Kano plucking rapeseed oil (nonhydratable phospholipids content be in the vegetables oil), acid value 1.8mgKOH/g, phosphorus content 650ppm.
Adopt following refinery practice refining:
Adopt the Degumming Procedures of embodiment 1 to prepare degummed oil (moisture＜0.1%), adopt board-like or tubular heat exchange adjustment temperature to 120 ℃), adding accounts for degummed oil weight 0.5% atlapulgite under the 150mbar absolute pressure; Through the decoloring reaction of 25min, get into filter and filter, the edible vegetable oil that comes out is again through the smart filter of insurance strainer; Decolouring edible vegetable oil gets into deacid-deodoring workshop section (stripping gas addition; Oil is heavy by 1%), decolouring edible vegetable oil at first with the processed oil heat exchange of coming out of deodorization tower, be heated to 260 ℃ through HP steam or other thermal source again; Get into deacid-deodoring tower; The decolouring edible vegetable oil FFA content that gets into deacid-deodoring tower is at 0.05%--4wt%, the absolute pressure＜2.5mbar of deacid-deodoring, and deodorization time is at 120min; Deacid-deodoring oil that comes out and the energy-conservation heat exchange of decolouring edible vegetable oil of advancing tower promptly obtain finished product RBD oil (final decoloration and deodorization processed oil) through last interchanger cooling and secondary filter again.
Detect: processed oil FFA content is 0.03%, processed oil color and luster Y12R1.2, and 218 ℃ of processed oil smoke points, the processed oil yield is 95.8%.
Claims (20)
1. the degumming technology of an edible vegetable oil for elder generation is converted into hydrated phospholipid with crude oil and acid-respons with the nonhydratable phosphatide in the crude oil, and after aquation is condensed micelle, obtains degummed oil through spinning again.
2. the degumming technology of edible vegetable oil according to claim 1 is characterized in that, specifically comprises the following steps:
1) transforms: be that 50--70 ℃ crude oil is with after the Hydrocerol A that accounts for crude oil weight 0.05-0.5%, phosphoric acid, oxysuccinic acid or oxalic acid mix with temperature; In the acid-respons jar stirring reaction 15-30 minute; Accomplish the reaction that nonhydratable phosphatide is converted into hydrated phospholipid, obtain transformation mixture;
2) aquation: after transformation mixture and the 20-50 ℃ of weight 1.5-2.5 soft water doubly that is phosphatide weight in the crude oil mixed, temperature adjustment was to 20-45 ℃, and in the hydration reaction jar stirring reaction 45-150 minute, the completion hydration reaction obtained hydrated mixt;
3) spinning: hydrated mixt is heated to 75-90 ℃ after the whizzer spinning, separates the thing that gently is separated that obtains and after vacuum precipitation drying, obtain degummed oil.
3. like the degumming technology of the said edible vegetable oil of claim 2, it is characterized in that in the step 1), the phosphorus content of said crude oil is 100-700ppm, impurity content＜0.2wt%.
4. like the degumming technology of the said edible vegetable oil of claim 2, it is characterized in that in the step 1), Hydrocerol A, phosphoric acid, oxysuccinic acid or oxalic acid account for crude oil weight 0.15-0.5%.
5. like the degumming technology of the said edible vegetable oil of claim 2, it is characterized in that step 2) in, said soft water is the soft water that is lower than 10 degree.
6. like the degumming technology of the said edible vegetable oil of claim 2, it is characterized in that step 2) in, the stirring velocity of stirring reaction is 35-75 rev/min in the said hydration reaction jar, the 45-120 minute hydration reaction residence time.
7. like the degumming technology of the said edible vegetable oil of claim 2, it is characterized in that in the step 3), the mixture heat exchange through the mixture elder generation of aquation passes through plate-type heat exchanger and water inletization retort is heated to 75-90 ℃ through board-like or tubular heat exchange again.
8. like the degumming technology of the arbitrary said edible vegetable oil of claim 1-7; It is characterized in that; In the step 3), the said thing that gently is separated can be first gently the be separated thing or separate second thing that gently is separated that obtains through the whizzer two times centrifugal that obtains through a spinning of whizzer.
9. like the degumming technology of the said edible vegetable oil of claim 8; It is characterized in that; Saidly be specially: hydrated mixt is heated to 75-90 ℃ after the first whizzer spinning obtains first thing that gently is separated through the isolating method of whizzer two times centrifugal; Said first gently the be separated soft water of thing weight 2.5-5% of thing and 75-90 ℃ account for said first that gently is separated is mixed; Oil-water mixture got into the washing of washing remaining tank after 10-30 minute, again through the second whizzer spinning, obtained second thing that gently is separated.
10. like the degumming technology of the said edible vegetable oil of claim 9, it is characterized in that, will be through the heavy phase isolate of the second whizzer spinning as step 2) in the soft water source.
11. the degumming technology like the said edible vegetable oil of claim 2 is characterized in that, in the step 3), before the thing vacuum that gently the is separated precipitation drying, is heated to 75-120 ℃.
12. the degumming technology like the said edible vegetable oil of claim 2 is characterized in that, in the step 3), the residual voltage when said vacuum precipitation is dry is 25-100mpa.
13. like the purposes of the said degumming technology of the arbitrary claim of claim 1-12 in the edible vegetable oil refinery practice.
14. an edible vegetable oil refinery practice comprises the following steps:
A. crude oil is adopted earlier the said degumming technology of the arbitrary claim of the claim 1-12 acquisition degummed oil that comes unstuck;
B. degummed oil without in directly decolour with depickling and to obtain decolouring edible vegetable oil;
C. decolour edible vegetable oil behind deacid-deodoring, obtain finished product RBD oil through cooling and smart filter.
15. like the said edible vegetable oil refinery practice of claim 14, it is characterized in that, in the step a), said degummed oil phosphorus content＜10ppm, moisture content＜0.1wt%.
16. like the said edible vegetable oil refinery practice of claim 14; It is characterized in that; In the step b), the method that said decolouring obtains decolouring edible vegetable oil is specially: said degummed oil is heated to 105-120 ℃, under the 50-150mbar absolute pressure, adds the atlapulgite that accounts for said degummed oil weight 0.5-2.0%; Behind 25-45 minute decoloring reaction, obtain decolouring edible vegetable oil through filtering successively with smart filter.
17., it is characterized in that in the step c), during deacid-deodoring, stripping gas adds the 0.3-1.5% of weight for decolouring edible vegetable oil weight like the said edible vegetable oil refinery practice of claim 14.
18., it is characterized in that in the step c), the method for said decolouring edible vegetable oil deacid-deodoring can be selected from following arbitrary like the said edible vegetable oil refinery practice of claim 14:
After I, the edible vegetable oil that will decolour are heated to 240-260 ℃, through the deacid-deodoring tower deacid-deodoring;
After II, the edible vegetable oil that will decolour are heated to 240-260 ℃, earlier through the extracting tower depickling, again through the deodorization of deodorization tower;
After III, the edible vegetable oil that will decolour are heated to 240-260 ℃, earlier through the deodorization of deodorization tower, again through the extracting tower depickling.
19. like the said edible vegetable oil refinery practice of claim 18; It is characterized in that, advance the tower deacid-deodoring before, decolouring edible vegetable oil FFA content is 0.05wt%--4wt%; Absolute pressure＜2.5mbar when depickling and deodorization, deacid-deodoring total time is 45min--120min.
20., it is characterized in that the heating means of decolouring edible vegetable oil are like the said edible vegetable oil refinery practice of claim 18: will decolour edible vegetable oil at first with the high temperature oil heat exchange that goes out tower through deacid-deodoring, pass through HP steam or other thermals source again and be heated to 240-260 ℃.
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