CN102533441B - 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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- CN102533441B CN102533441B CN201210019949.7A CN201210019949A CN102533441B CN 102533441 B CN102533441 B CN 102533441B CN 201210019949 A CN201210019949 A CN 201210019949A CN 102533441 B CN102533441 B CN 102533441B
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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 edible oil manufacture field, be specifically related to degumming technology and the application thereof of edible vegetable oil.
Background technology
The production of all edible vegetable oils all will come by refining procedure processing such as degumming raw oil, removing impurities, depickling, precipitation, dry, decolouring, deodorization and winterisations, difference due to crude oil kind and processed oil class requirement, the procedure technology of the course of processing may 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 is all absolutely necessary in each technique.
The degumming technology that current line exists in the industry comprises that water comes unstuck, special coming unstuck and enzymatic degumming.Wherein, the defect that water comes unstuck is to remove nonhydratable phosphatide; It is not thorough that special defect of coming unstuck is that phosphatide removes, and phosphorus content is greater than 20ppm; The removal effect of enzymatic degumming is good, but defect is the on the high side of enzyme, and production cost is high relatively.
The direct or indirect technological effect that affects 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 by and depickling or reach degumming effect comparatively completely by the auxiliary degumming effect that atlapulgite is added in decolouring, yet this unavoidable auxiliary degumming processing certainly will reduce product yield, increase the consumption of supplementary material and neutral oil, but also can increase the possibility of sewage discharge.
Edible vegetable oil physical refining process is to be only used in the palmitic processing that gel content is low 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 no the degumming technology of economic and reliable, large industrialized is produced all will adopt chemical refining operation substantially in order to reach necessary degumming effect.
Summary of the invention
Object of the present invention overcomes defect of the prior art exactly, and a kind of degumming technology and application thereof of edible vegetable oil are provided.
First the present invention discloses a kind of degumming technology of edible vegetable oil, for first crude oil and acid-respons being converted into hydrated phospholipid by the nonhydratable phosphatide in crude oil, and by aquation cohesion micelle, then obtain degummed oil through centrifugation.
Concrete, described degumming technology comprises the following steps:
1) transform: by temperature, be after the crude oil of 50--70 ℃ mixes with the citric acid, phosphoric acid, oxysuccinic acid or the oxalic acid that account for crude oil weight 0.05-0.5%, stirring reaction 15-30 minute in acid-respons tank, complete the reaction that nonhydratable phosphatide is converted into hydrated phospholipid, obtain transformation mixture;
2) aquation: after the 1.5-2.5 that is phosphatide weight in crude oil with 20-50 ℃ of weight by transformation mixture soft water doubly mixes, temperature adjustment is to 20-45 ℃, and stirring reaction 45-150 minute, completes hydration reaction in hydration reaction tank, obtains hydrated mixt;
3) centrifugation: hydrated mixt is heated to 75-90 ℃ by whizzer centrifugation, and the thing that is gently separated that separation obtains obtains degummed oil after vacuum desolvation is dry.
More specifically:
Step 1) in,
Described 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).
Preferably, the phosphorus content of described 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 ℃.
Acid used can be selected from citric acid, phosphoric acid, oxysuccinic acid, oxalic acid.Preferably, citric acid, phosphoric acid, oxysuccinic acid or oxalic acid account for crude oil weight 0.15-0.5%.
As cited in the embodiment of the present invention, acid can first configure after aqueous acid, adds in proportion.The aqueous citric acid solution that for example adds 50wt%.
In described acid-respons tank, the stirring velocity general control of stirring reaction is 45-60 rev/min.
Through step 1), in crude oil, nonhydratable phosphatide is converted into the reactivity > 99.5% of hydrated phospholipid.
Step 2) in,
Described soft water is the soft water lower than 10 degree (German degree).
After described transformation mixture mixes with described soft water, can adopt the cooling temperature adjustment of plate-type heat exchanger.
In described hydration reaction tank, the stirring velocity general control of stirring reaction is 35-75 rev/min, and the hydration reaction residence time can be 45-150 minute, and general control is 45-120 minute.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, crude oil phosphorus content is high or temperature of reaction is high, can agitation as appropriate hurry up, the temperature of reaction low reaction time is long.
Step 3) in,
The described mixture through aquation can be through board-like or tubular heat exchange or heater heats to 75-90 ℃.
Preferably, through the first mixture heat exchange with water inletization retort by plate-type heat exchanger of mixture of aquation, then be heated to 75-90 ℃ by board-like or tubular heat exchange, this design can be further energy-conservation.
The described thing that is gently separated can be the first be gently the separated thing or through separated second thing that is gently separated obtaining of whizzer two times centrifugal obtaining through a centrifugation of whizzer.
The described method through the separation of whizzer two times centrifugal is specially: hydrated mixt is heated to 75-90 ℃ and by the first whizzer centrifugation, obtains first thing that is gently separated, described first be gently the separated soft water of thing weight 2.5-5% of thing and 75-90 ℃ account for described first that is gently separated is mixed, oil-water mixture entered the washing of washing remaining tank after 10-30 minute, again through the second whizzer centrifugation, obtain second thing that is gently separated.Large at crude oil impurity content, crude oil phospholipids content is relatively high, and degummed oil phosphorus content is required, in relatively not high and the not enough situation of separate unit whizzer separating power, can adopt two times centrifugal separated.The in the situation that of only production level Four degummed oil and one bench centrifuge separating power abundance, only need a centrifugation.
In described two times centrifugal separation, when oil-water mixture enters the washing of washing remaining tank, can follow stirring, stirring velocity can be fast or slow, the general controlled 0-60 rev/min that is made as simultaneously.Described soft water is the soft water lower than 10 degree (German degree).
Centrifugation whizzer used can adopt disk plate centrifuge.
Preferably, in order to exempt the processing of heavy phase isolate (being waste water) after centrifugation, can be using the heavy phase isolate through the second whizzer centrifugation as step 2) in soft water source.This step not only can water saving, also can reduce processing and the discharge of waste water.
Further, before the thing vacuum desolvation that is gently separated is dry, 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 is gently separated has reached temperature requirement (more than 75 ℃), and this step can be omitted.
Residual voltage when preferably, described vacuum desolvation is dry is 25-100mpa.Can be dried to moisture content < 0.1wt%.Precipitation is to the residual molten < 30ppm that is down to.
Vacuum desolvation is dry can adopt vacuum drier to carry out, as spraying drying type or baffle plate overflow type vacuum drier.
Degumming method of the present invention is changed nonhydratable phosphatide by acid-respons, rehydration cohesion micelle, by whizzer separated (conversion-aquation-centrifugation), it is qualified that the degummed oil phosphorus content obtaining can reach 280 ℃ of Heating Experiments of GB, the phosphorus content index < 10ppm of degummed oil, needn't pass through the Zhong He workshop section of chemical refining and directly enter decoloration and deodorization workshop section, can adopt the operational path of physical refining to produce primary oil completely.
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 refined oil technique, comprises the following steps:
A. crude oil is first adopted to the degumming technology of the present invention acquisition degummed oil that comes unstuck;
B. degummed oil without in and depickling direct bleaching obtain decolouring edible vegetable oil;
C. decolour edible vegetable oil after deacid-deodoring, through cooling and smart filter, obtain finished product RBD oil (refining decoloration and deodorization oil).
Concrete,
Step a) in,
Described degummed oil phosphorus content < 10ppm, moisture content < 0.1wt%.
If degummed oil moisture content >=0.1wt%, step a) increases drying step, makes degummed oil moisture content < 0.1wt%.
Step b) in,
Described decolouring can adopt decoloration process one time, for reducing Clay consumption, also can adopt secondary decolourization technique (also claiming pre-de-de-technique again).
Preferably, the method that described decolouring obtains decolouring edible vegetable oil is specially: described degummed oil is heated to 105-120 ℃, under 50-150mbar absolute pressure, add the atlapulgite that accounts for described degummed oil weight 0.5-2.0%, after the decoloring reaction of 25-45 minute, filter obtains decolouring edible vegetable oil with essence after filtration successively.
Degummed oil can adopt board-like or tubular heat exchange or heater heats to 105-120 ℃.
Filtration can adopt filter, and smart filter can adopt insurance strainer.
Step c) in,
Preferably, during deacid-deodoring, stripping gas adds weight for the 0.3-1.5% of decolouring edible vegetable oil weight, is more preferred from 0.3-1.0%.
Concrete, the method for described decolouring edible vegetable oil deacid-deodoring can be selected from following arbitrary:
I, decolouring edible vegetable oil is heated to after 240-260 ℃, through deacid-deodoring tower deacid-deodoring;
II, decolouring edible vegetable oil is heated to after 240-260 ℃, first through extracting tower depickling, then through deodorizing tower deodorization;
III, decolouring edible vegetable oil is heated to after 240-260 ℃, first through deodorizing tower deodorization, then through extracting tower depickling;
Preferably, method I) in, the depickling of described deacid-deodoring tower partly adopts structured packing tower structure, and deodorization partly adopts tray column structure.The packing tower of described deacid-deodoring tower can be formerly, rear or in centre.
Preferably, enter before tower deacid-deodoring, 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 be 45min--120min (wherein, the depickling time is shorter, is generally no more than 5min).
Preferably, the heating means of decolouring edible vegetable oil are: by decolouring edible vegetable oil first with the high temperature oil heat exchange that goes out tower through deacid-deodoring, then be heated to 240-260 ℃ through high pressure steam or other thermal source.This measure, can be further energy-conservation.
Refined oil technique of the present invention successively through coming unstuck, decolouring, deacid-deodoring (distillation method disacidify) obtain RBD processed oil, whole process, without in alkali refining separately and depickling step, is physical refining.
Beneficial effect of the present invention:
Degumming process for edible vegetable oil 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 feature of degumming effect is more outstanding, this is not singly the innovation aspect fat degumming, and the progress of this kind of degumming technology has driven and produces novel grease processing physics refining techniques.
Refined oil technique of the present invention is abandoned chemical refining and is adopted the advantage of physical refining to be:
1) yield that can improve processed oil is (rapeseed oil improves yield 0.8%--1%, soybean oil improves yield 0.6%--0.8%) approximately;
2) do not had in and the discharge of washing water waste water (6% left and right of the chemical refining washing sewage flow rate amount of accounting for conventionally);
3) adopt physical refining there is no the processing costs of phosphorous soap stock, (lipid acid output improves about rapeseed oil 1% to have improved the quantity and quality of high value byproduct deodorised fat acid, soya-bean oil 0.8%, the FFA of lipid acid is increased to 75% by 50% content), the auxiliary materials such as other carclazyte are used suitable with chemical refining.
Embodiment
Below enumerate specific embodiment further to set forth the present invention, should be understood that example is not for limiting the scope of the invention.
Embodiment 1
Raw material: Canadian Kano is drawn and leached Crude Dapeseed Oil one of (nonhydratable phospholipids content be in vegetables oil the highest), acid value 1.8mgKOH/g, phosphorus content 650ppm.
Adopt following technique 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 50wt% aqueous citric acid solution that cutter formula or centrifugal mixer add concentration, until citric acid accounts for crude oil weight 0.28%, enter the retort of belt stirrer, stirring velocity 45-60 rev/min, in 30 minutes reaction times, after reaction, nonhydratable phosphatide is converted into the 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 water cooling by plate-type heat exchanger heat exchange, oil temperature 35 ℃ water--oil enters hydration reaction tank.Hydration reaction tank belt stirrer rotating speed 35-75 rev/min, 90 minutes hydration reaction residence time.By hydration reaction tank, reaction mixture is the mixture heat exchange with water inletization retort by plate-type heat exchanger, by board-like or tubular heat exchange, be heated to 85 ℃ again, by disk plate centrifuge separation, obtain light phase degummed oil and by cutter formula or centrifugal mixer, add the soft water (85 ℃ of soft water temperature) of degummed oil weight 2.5%, oil-water enters washing remaining tank, 25 minutes residence time, then by washing oil pump oil-water mixture, enter the second bench centrifuge, gently be separated thing degumming water washing oil again (words that oil temperature is low are heated to 88 ℃ by tubulation or plate heater) enter precipitation moisture eliminator, precipitation moisture eliminator is worked under 25-100mpa residual voltage, go out precipitation moisture eliminator and obtain degummed oil.
Detect: degummed oil phosphorus content 8ppm, 280 ℃ of Heating Experiments are without separating 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 technique to come unstuck:
Normal temperature Crude Dapeseed Oil is (containing assorted < 0.2%, FFA content 0.9%) board-like or tubular heat exchange (well heater) is heated to 65 ℃, it is 50wt% aqueous citric acid solution that cutter formula or centrifugal mixer add concentration, until citric acid accounts for crude oil weight 0.28%, enter the retort of belt stirrer, stirring velocity 45-60 rev/min, in 30 minutes reaction times, after reaction, nonhydratable phosphatide is converted into the 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 water cooling by plate-type heat exchanger heat exchange, oil temperature 35 ℃ water--oil enters hydration reaction tank.Hydration reaction tank belt stirrer rotating speed 35-75 rev/min, 90 minutes hydration reaction residence time.By hydration reaction tank, reaction mixture is the mixture heat exchange with water inletization retort by plate-type heat exchanger, by board-like or tubular heat exchange, be heated to 85 ℃ again, by disk plate centrifuge separation, obtain light phase degummed oil (words that oil temperature is low are heated to 85 ℃ by tubulation or plate heater) and enter precipitation moisture eliminator, precipitation moisture eliminator is worked under 25-100mpa residual voltage, goes out precipitation moisture eliminator and obtains degummed oil.
Detect: degummed oil phosphorus content 15ppm, 280 ℃ of Heating Experiments are without separating 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 technique 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 50wt% aqueous citric acid solution that cutter formula or centrifugal mixer add concentration, until citric acid accounts for crude oil weight 0.15%, enter the retort of belt stirrer, stirring velocity 45-60 rev/min, in 15 minutes reaction times, after reaction, nonhydratable phosphatide is converted into the 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 water cooling by plate-type heat exchanger heat exchange, oil temperature 20 ℃ water--oil enters hydration reaction tank.Hydration reaction tank belt stirrer rotating speed 35-75 rev/min, 45 minutes hydration reaction residence time.By hydration reaction tank, reaction mixture is the mixture heat exchange with water inletization retort by plate-type heat exchanger, by board-like or tubular heat exchange, be heated to 75 ℃ again, by disk plate centrifuge separation, obtain light phase degummed oil and by cutter formula or centrifugal mixer, add the soft water (75 ℃ of soft water temperature) of degummed oil weight 2.5-5%, oil-water enters washing remaining tank, 60 revs/min of water washing tank stirring velocitys, 10 minutes time, then by washing oil pump oil-water mixture, enter the second bench centrifuge, gently be separated thing degumming water washing oil again (words that oil temperature is low are heated to 110 ℃ by tubulation or plate heater) enter precipitation moisture eliminator, precipitation moisture eliminator is worked under 100mpa residual voltage, go out precipitation moisture eliminator and obtain degummed oil.
Detect: degummed oil phosphorus content 9ppm, 280 ℃ of Heating Experiments are without separating 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 technique to come unstuck:
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 50wt% aqueous citric acid solution that cutter formula or centrifugal mixer add concentration, until citric acid accounts for crude oil weight 0.5%, enter the retort of belt stirrer, stirring velocity 45-60 rev/min, in 25 minutes reaction times, after reaction, nonhydratable phosphatide is converted into the 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 water cooling by plate-type heat exchanger heat exchange, oil temperature 45 ℃ water--oil enters hydration reaction tank.Hydration reaction tank belt stirrer rotating speed 35-75 rev/min, 120 minutes hydration reaction residence time.By hydration reaction tank, reaction mixture is the mixture heat exchange with water inletization retort by plate-type heat exchanger, by board-like or tubular heat exchange, be heated to 90 ℃ again, by disk plate centrifuge separation, obtain light phase degummed oil and by cutter formula or centrifugal mixer, add the soft water (90 ℃ of soft water temperature) of degummed oil weight 2.5-5%, oil-water enters washing remaining tank, 30 minutes time, then by washing oil pump oil-water mixture, enter the second bench centrifuge, gently be separated thing degumming water washing oil again (words that oil temperature is low are heated to 88 ℃ by tubulation or plate heater) enter precipitation moisture eliminator, precipitation moisture eliminator is worked under 25mpa residual voltage, go out precipitation moisture eliminator and obtain degummed oil.
Detect: degummed oil phosphorus content 6ppm, 280 ℃ of Heating Experiments are without separating 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, containing assorted 0.1%.
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 110 ℃, under 100mbar absolute pressure, add and account for degummed oil weight 1% atlapulgite, decoloring reaction through 35min, entering filter filters, edible vegetable oil is out again through the filter of insurance strainer essence, decolouring edible vegetable oil enters deacid-deodoring workshop section (stripping gas addition, oil is heavy by 0.8%), decolouring edible vegetable oil first with out processed oil heat exchange of deodorizing tower, through high pressure steam or other thermal source, be heated to 258 ℃ again, enter deacid-deodoring tower, enter the decolouring edible vegetable oil FFA content of deacid-deodoring tower at 1.2wt%, the absolute pressure 2.2mbar of deacid-deodoring, deodorization time is at 90min, deacid-deodoring oil and the energy-conservation heat exchange of decolouring edible vegetable oil of entering tower out, and secondary filter cooling through last interchanger obtain finished product RBD oil (final decoloration and deodorization processed oil) 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 in 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, it is 95.1% that the processed oil yield=processed oil quality/quality of crude oil of take calculates processed oil yield.
Embodiment 6
Raw material: Canadian Kano is drawn and leached Crude Dapeseed Oil (nonhydratable phospholipids content be in 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 105 ℃, under 50mbar absolute pressure, add and account for degummed oil weight 2.0% atlapulgite, decoloring reaction through 45min, entering filter filters, edible vegetable oil is out again through the filter of insurance strainer essence, decolouring edible vegetable oil enters deacid-deodoring workshop section (stripping gas addition, oil is heavy by 0.3%), decolouring edible vegetable oil first with out processed oil heat exchange of deodorizing tower, through high pressure steam or other thermal source, be heated to 240 ℃ again, enter deacid-deodoring tower, enter the decolouring edible vegetable oil FFA content of deacid-deodoring tower at 1.2wt%, the absolute pressure < 2.5mbar of deacid-deodoring, deodorization time is at 45min, deacid-deodoring oil and the energy-conservation heat exchange of decolouring edible vegetable oil of entering tower out, and secondary filter cooling through last interchanger obtain finished product RBD oil (final decoloration and deodorization processed oil) again.
Detect: processed oil FFA content is 0.045%, processed oil color and luster Y10R0.8,216 ℃ of processed oil smoke points, processed oil yield is 95.45%.
Embodiment 7
Raw material: Canadian Kano plucking rapeseed oil (nonhydratable phospholipids content be in 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 ℃), under 150mbar absolute pressure, add and account for degummed oil weight 0.5% atlapulgite, decoloring reaction through 25min, entering filter filters, edible vegetable oil is out again through the filter of insurance strainer essence, decolouring edible vegetable oil enters deacid-deodoring workshop section (stripping gas addition, oil is heavy by 1%), decolouring edible vegetable oil first with out processed oil heat exchange of deodorizing tower, through high pressure steam or other thermal source, be heated to 260 ℃ again, enter deacid-deodoring tower, enter the decolouring edible vegetable oil FFA content of deacid-deodoring tower at 0.05%--4wt%, the absolute pressure < 2.5mbar of deacid-deodoring, deodorization time is at 120min, deacid-deodoring oil and the energy-conservation heat exchange of decolouring edible vegetable oil of entering tower out, and secondary filter cooling through last interchanger obtain finished product RBD oil (final decoloration and deodorization processed oil) again.
Detect: processed oil FFA content is 0.03%, processed oil color and luster Y12R1.2,218 ℃ of processed oil smoke points, processed oil yield is 95.8%.
Claims (17)
1. a refined oil technique, comprises the following steps:
A. crude oil is first adopted to the degumming technology acquisition degummed oil that comes unstuck, described degumming technology is for to be first converted into hydrated phospholipid by crude oil and acid-respons by the nonhydratable phosphatide in crude oil, and by aquation cohesion micelle, then obtain degummed oil through centrifugation; Described degumming technology specifically comprises the following steps:
1) transform: by temperature, be after the crude oil of 50--70 ℃ mixes with the citric acid, phosphoric acid, oxysuccinic acid or the oxalic acid that account for crude oil weight 0.05-0.5%, stirring reaction 15-30 minute in acid-respons tank, complete the reaction that nonhydratable phosphatide is converted into hydrated phospholipid, obtain transformation mixture;
2) aquation: after the 1.5-2.5 that is phosphatide weight in crude oil with 20-50 ℃ of weight by transformation mixture soft water doubly mixes, temperature adjustment is to 20-45 ℃, and stirring reaction 45-150 minute, completes hydration reaction in hydration reaction tank, obtains hydrated mixt;
3) centrifugation: hydrated mixt is heated to 75-90 ℃ by whizzer centrifugation, and the thing that is gently separated that separation obtains obtains degummed oil after vacuum desolvation is dry;
B. degummed oil without in and depickling direct bleaching obtain decolouring edible vegetable oil;
C. decolour edible vegetable oil after deacid-deodoring, through cooling and smart filter, obtain finished product RBD oil.
2. refined oil technique as claimed in claim 1, is characterized in that, in step 1), the phosphorus content of described crude oil is 100-700ppm, impurity content < 0.2wt%.
3. refined oil technique as claimed in claim 1, is characterized in that, in step 1), citric acid, phosphoric acid, oxysuccinic acid or oxalic acid account for crude oil weight 0.15-0.5%.
4. refined oil technique as claimed in claim 1, is characterized in that step 2) in, described soft water is the soft water lower than 10 degree.
5. refined oil technique as claimed in claim 1, is characterized in that step 2) in, in described hydration reaction tank, the stirring velocity of stirring reaction is 35-75 rev/min, hydration reaction residence time 45-120 minute.
6. refined oil technique as claimed in claim 1, is characterized in that, in step 3), through the first mixture heat exchange with water inletization retort by plate-type heat exchanger of mixture of aquation, then is heated to 75-90 ℃ by board-like or tubular heat exchange.
7. refined oil technique as described in as arbitrary in claim 1-6, it is characterized in that, in step 3), the described thing that is gently separated can be the first be gently the separated thing or through separated second thing that is gently separated obtaining of whizzer two times centrifugal obtaining through a centrifugation of whizzer.
8. refined oil technique as claimed in claim 7, it is characterized in that, the described method through the separation of whizzer two times centrifugal is specially: hydrated mixt is heated to 75-90 ℃ and by the first whizzer centrifugation, obtains first thing that is gently separated, described first be gently the separated soft water of thing weight 2.5-5% of thing and 75-90 ℃ account for described first that is gently separated is mixed, oil-water mixture entered the washing of washing remaining tank after 10-30 minute, again through the second whizzer centrifugation, obtain second thing that is gently separated.
9. refined oil technique as claimed in claim 8, is characterized in that, using the heavy phase isolate through the second whizzer centrifugation as step 2) in soft water source.
10. refined oil technique as claimed in claim 1, is characterized in that, in step 3), before the thing vacuum desolvation that is gently separated is dry, is heated to 75-120 ℃.
11. refined oil techniques as claimed in claim 1, is characterized in that, in step 3), residual voltage when described vacuum desolvation is dry is 25-100mpa.
12. refined oil techniques as claimed in claim 1, is characterized in that, in step a), and described degummed oil phosphorus content < 10ppm, moisture content < 0.1wt%.
13. refined oil techniques as claimed in claim 1, it is characterized in that, in step b), the method that described decolouring obtains decolouring edible vegetable oil is specially: described degummed oil is heated to 105-120 ℃, under 50-150mbar absolute pressure, add the atlapulgite that accounts for described degummed oil weight 0.5-2.0%, after the decoloring reaction of 25-45 minutes, filter obtains decolouring edible vegetable oil with essence after filtration successively.
14. refined oil techniques as claimed in claim 1, is characterized in that step c) in, during deacid-deodoring, stripping gas adds weight for the 0.3-1.5% of decolouring edible vegetable oil weight.
15. refined oil techniques as claimed in claim 1, is characterized in that step c) in, the method for described decolouring edible vegetable oil deacid-deodoring can be selected from following arbitrary:
I, decolouring edible vegetable oil is heated to after 240-260 ℃, through deacid-deodoring tower deacid-deodoring;
II, decolouring edible vegetable oil is heated to after 240-260 ℃, first through extracting tower depickling, then through deodorizing tower deodorization;
III, decolouring edible vegetable oil is heated to after 240-260 ℃, first through deodorizing tower deodorization, then through extracting tower depickling.
16. refined oil techniques as claimed in claim 15, is characterized in that, enter before tower deacid-deodoring, and decolouring edible vegetable oil FFA content is 0.05wt%--4wt%, absolute pressure < 2.5mbar when depickling and deodorization, and deacid-deodoring total time is 45min--120min.
17. refined oil techniques as claimed in claim 15, is characterized in that, the heating means of decolouring edible vegetable oil are: by decolouring edible vegetable oil first with the high temperature oil heat exchange that goes out tower through deacid-deodoring, then be heated to 240-260 ℃ through high pressure steam or other thermals source.
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