CN107418725B - Refining process of crude oil with ultrahigh acid value - Google Patents
Refining process of crude oil with ultrahigh acid value Download PDFInfo
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- CN107418725B CN107418725B CN201710595050.2A CN201710595050A CN107418725B CN 107418725 B CN107418725 B CN 107418725B CN 201710595050 A CN201710595050 A CN 201710595050A CN 107418725 B CN107418725 B CN 107418725B
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/001—Refining fats or fatty oils by a combination of two or more of the means hereafter
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/008—Refining fats or fatty oils by filtration, e.g. including ultra filtration, dialysis
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/02—Refining fats or fatty oils by chemical reaction
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/02—Refining fats or fatty oils by chemical reaction
- C11B3/04—Refining fats or fatty oils by chemical reaction with acids
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/02—Refining fats or fatty oils by chemical reaction
- C11B3/06—Refining fats or fatty oils by chemical reaction with bases
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- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/16—Refining fats or fatty oils by mechanical means
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Abstract
The invention discloses a refining process of crude oil with ultrahigh acid value, which comprises the following steps: (1) heating the super-high acid value crude oil to 50 ℃, and adding 75% or 85% of phosphoric acid according to the amount of 3-4kg of crude oil per ton; (2) adding NaOH solution through a mixer; (3) adding NaCl solution according to 5% of the crude oil, heating, and removing soap; (4) adding a citric acid solution according to 0.05 percent of the mass of the crude oil, and adding a NaCl solution; (5) oil obtained after NaCl solution is evenly mixed is subjected to oil-water separation and vacuum drying; (6) heating the drying oil, and carrying out vacuum decolorization; (7) heating the decolorized oil, continuously heating after deacidification, and entering a plate tower or a packed tower for deodorization; (8) and adding citric acid solution into the cooled deodorized oil, and checking to be qualified to obtain a finished product. The invention has the beneficial effects that: by adopting the method, the production efficiency and the refining yield are effectively improved, and the emulsification problem in the refining process of the crude oil with the ultrahigh acid value is effectively solved.
Description
Technical Field
The invention relates to the field of refining of crude oil with ultrahigh acid value, and mainly relates to a refining process of crude oil with ultrahigh acid value.
Background
The super-high acid value crude oil refers to crude oil with the acid value of more than 10mm/gKOH, and the acid value is generally 10-30 mm/gKOH. The existing refining technology of the crude oil with high acid value adopts the following steps: the high acid value crude oil is hydrated and degummed, and then is washed, decolorized and deacidified. By adopting the existing method, because the high acid value oil is seriously emulsified in the degumming and water washing processes, the degumming effect is poor and the loss is serious; because the acid value of the degummed oil is too high and the quality of the degummed oil is too poor, the argil is easy to be poisoned in the decoloring process, the consumption of the argil is too large, the loss of micro-nutrient components in the oil is too large, and the decoloring effect is poor; because the degumming and decoloring effects are poor, and the acid value of the decolored oil is too high, the deodorization process is too long, the nutrition loss is huge, the decolored oil is serious in color reversion, the quality of the refined oil is not good enough, and the processing cost is high; due to the serious color reversion, the secondary refining is frequent, so that the economic benefit is further reduced, and the product quality cannot be effectively improved.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provides a process for refining crude oil with ultrahigh acid value, in particular to a method for carrying out acid reaction on the crude oil with ultrahigh acid value, alkali refining, water washing, drying, decoloring and low-temperature deodorization. After processing, the quality and the refining yield of the oil are effectively improved, the production efficiency is also effectively improved, and the production cost is reduced.
The object of the present invention is achieved by the following technical means. The refining process of the crude oil with the ultrahigh acid value comprises the following steps:
(1) heating the crude oil with ultrahigh acid value to 50 ℃, adding 75% or 85% of phosphoric acid according to the amount of 3-4kg of crude oil per ton, and stirring for reaction for 30-60 min;
(2) adding 22-24% NaOH solution through a mixer according to the alkali adding amount for removing acid value of 5mg/gKOH, and continuously stirring for reacting for 20-30 min;
(3) adding 10% NaCl solution according to 10% of the crude oil, continuously stirring for 10min, heating to 75-80 deg.C, and removing soap;
(4) after soaping, adding 50% citric acid solution according to 0.05% of the mass of the crude oil, continuously stirring for 30min, and adding 10% NaCl solution according to 10% of the mass of the crude oil, wherein the temperature of the NaCl solution is 80-85 ℃;
(5) oil obtained after NaCl solution is evenly mixed is subjected to oil-water separation and vacuum drying, and the vacuum degree of a dryer is 10-20 mmHg;
(6) heating the drying oil to 100-110 deg.C, vacuum decolorizing for 25-35 min;
(7) heating the decolorized oil to 210-220 ℃, delivering the decolorized oil to a deacidification tower for deacidification, continuously heating the deacidified oil to 235-250 ℃ for deodorization in a plate tower or a packed tower;
(8) and adding 50% citric acid solution into the cooled deodorized oil according to the mass of 0.005% -0.01% of the deodorized oil, quickly mixing, polishing, filtering, and checking to obtain the finished product.
Furthermore, in the step (1), the super-high acid value crude oil is heated to 50 ℃, 75% or 85% phosphoric acid is added according to the amount of 3-4kg of crude oil per ton, and after rapid stirring, the stirring reaction is continued for 30-60 min.
Further, in the step (3), the soaping is carried out by standing, precipitating or centrifuging.
The invention has the beneficial effects that: compared with the prior art, the invention adopts alkali refining and water washing technology for preventing emulsification, decoloration technology for preventing color reversion and deodorization technology with lower strength. By adopting the prior art, the refining yield can approach the theoretical level, the micro-nutrient content is effectively improved, and the product can completely reach the national standard or the standard level; compared with the prior high acid value oil refining technology, the invention not only greatly improves the product quality, but also effectively improves the micro-nutrient content of the product. Compared with the prior refining technology, the technology has the advantages that the technology combining dry alkali refining and physical refining is adopted, the priority of the two technologies is fully exerted, the difficulty of the processing process is reduced, the quality of the intermediate product in the processing process is effectively improved, the production efficiency of the processing process is greatly improved, the production cost is effectively reduced, and the technology has popularization value.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The invention will be described in detail below with reference to the following drawings:
degumming the super-high acid value crude oil:
heating the crude oil with ultrahigh acid value to 50 ℃, adding 75% or 85% of phosphoric acid according to the amount of 3-4kg of crude oil per ton, rapidly stirring, and continuously stirring for reaction for 30-60 min; adding 22-24% NaOH solution through a mixer according to the alkali adding amount for removing acid value of 5mg/gKOH, and continuously stirring for reacting for 20-30 min; adding 10% NaCl solution according to 10% of crude oil amount, continuously stirring for 10min, heating to 75-80 deg.C, and removing soap (standing for precipitation or centrifuging); after the soaping is removed, 50% citric acid solution is added according to 0.05% of the crude oil amount, 10% NaCl solution is added according to 10% of the crude oil amount after continuous stirring for 30min, and the temperature of the NaCl solution is 80-85 ℃.
Physical refining:
oil obtained after NaCl solution is evenly mixed is subjected to oil-water separation and vacuum drying, and the vacuum degree of a dryer is 10-20 mmHg; heating the drying oil to 100-110 deg.C, vacuum decolorizing for 25-35 min; heating the decolorized oil to 210-220 ℃, delivering the decolorized oil to a deacidification tower for deacidification, continuously heating the deacidified oil to 235-250 ℃ for deodorization in a plate tower or a packed tower; and adding 50% citric acid solution into the cooled deodorized oil according to the amount of 0.005% -0.01% of the deodorized oil, quickly mixing, polishing, filtering, and inspecting to obtain the finished product.
Adding the super-high acid value crude oil into a food grade auxiliary material for preventing emulsification, fully mixing and reacting, and then carrying out dry alkali refining, thereby realizing good degumming and effectively removing free fatty acid in the crude oil; continuously adding auxiliary materials for preventing emulsification into the alkali refined oil, and adding saline water with certain concentration capable of resisting emulsification for washing; and (3) after the washing oil is dried, adding a proper amount of citric acid solution for preventing color reversion, fully mixing and reacting, decoloring, and deodorizing, thereby finishing the refining of the ultrahigh-acid-value crude oil. Because the dry alkali refining process and the water washing process which can prevent emulsification are adopted, the abnormal loss of the refining process is avoided, and the production efficiency and the yield are improved; because free fatty acid is basically removed after alkali refining, the problem of carclazyte poisoning caused by high acid value of degummed oil during decolorization is solved, and citric acid is added before decolorization and then decolorization is carried out, so that the consumption of a decolorizer is obviously reduced, the quality of decolorized oil is better, and the micro-nutrition loss in the decolorization process is lower; because the deodorization effect is good, the deodorization time and intensity are reduced, the deodorization oil loss and the micro-nutrient loss are obviously reduced, the production cost is effectively reduced, and the market competitiveness and the application range of products are improved.
Example 1: heating the crude oil with ultrahigh acid value to 50 ℃, adding 75% or 85% of phosphoric acid according to the amount of 4kg of crude oil per ton, rapidly stirring, and continuing stirring for reaction for 30 min; adding 22% NaOH solution through a mixer according to the alkali adding amount for removing the acid value of 5mg/gKOH, and continuously stirring and reacting for 30 min; adding 10% NaCl solution according to 10% of crude oil, continuously stirring for 10min, heating to 75 deg.C, and removing soap (standing for precipitation or centrifuging); after the soaping, adding 50% citric acid solution according to 0.05% of the mass of the crude oil, continuously stirring for 30min, and adding 10% NaCl solution according to 10% of the mass of the crude oil, wherein the temperature of the NaCl solution is 80 ℃. Oil obtained after NaCl solution is uniformly mixed is subjected to oil-water separation and vacuum drying, and the vacuum degree of a dryer is 20 mmHg; heating the drying oil to 100 deg.C, and vacuum decolorizing for 25 min; heating the decolorized oil to 210 ℃, delivering the decolorized oil to a deacidification tower for deacidification, continuously heating the deacidification oil to 240 ℃, and entering a plate tower or a packed tower for deodorization; and adding 50% citric acid solution into the cooled deodorized oil according to the amount of 0.006% of the deodorized oil, quickly mixing, polishing, filtering, and checking to obtain the finished product.
Example 2: heating the crude oil with ultrahigh acid value to 50 ℃, adding 75% or 85% of phosphoric acid according to the amount of 3kg of crude oil per ton, rapidly stirring, and continuing stirring for reaction for 60 min; adding 24% NaOH solution through a mixer according to the alkali adding amount for removing the acid value of 5mg/gKOH, and continuously stirring and reacting for 20 min; adding 10% NaCl solution according to 10% of crude oil, continuously stirring for 10min, heating to 80 deg.C, and removing soap (standing for precipitation or centrifuging); after the soaping, adding 50% citric acid solution according to 0.05% of the mass of the crude oil, continuously stirring for 30min, and adding 10% NaCl solution according to 10% of the mass of the crude oil, wherein the temperature of the NaCl solution is 85 ℃. Oil obtained after NaCl solution is evenly mixed is subjected to oil-water separation and vacuum drying, and the vacuum degree of a dryer is 10 mmHg; heating the drying oil to 110 deg.C, and vacuum decolorizing for 35 min; heating the decolorized oil to 220 ℃, delivering the decolorized oil into a deacidification tower for deacidification, continuously heating the decolorized oil to 245 ℃ after deacidification, and entering a plate tower or a packed tower for deodorization; and adding 50% citric acid solution into the cooled deodorized oil according to the amount of 0.008% of the deodorized oil, quickly mixing, polishing, filtering, and checking to obtain the finished product.
The refined oil after the process is adopted meets the national standard or the industrial standard. After the method is adopted, the production efficiency and the refining yield are effectively improved, and the emulsification problem in the refining process of the crude oil with the ultrahigh acid value is effectively solved; the method is not only suitable for refining various crude oils with ultrahigh acid value, such as walnut crude oil, peony seed crude oil, rice bran crude oil, gardenia crude oil and the like, but also suitable for refining easily emulsified crude oil in the refining process, such as corn crude oil, camellia seed crude oil and the like; after the method is adopted, the theoretical refining yield is approached, and the processing cost and the quality of the refined oil are effectively improved.
It should be understood that equivalent substitutions and changes to the technical solution and the inventive concept of the present invention should be made by those skilled in the art to the protection scope of the appended claims.
Claims (3)
1. A refining process of crude oil with ultrahigh acid value is characterized in that: the method comprises the following steps:
(1) heating the crude oil with ultrahigh acid value to 50 ℃, adding 75% or 85% of phosphoric acid according to the amount of 3-4kg of crude oil per ton, and stirring for reaction for 30-60 min;
(2) adding 22-24% NaOH solution through a mixer according to the alkali adding amount for removing acid value of 5mg/gKOH, and continuously stirring for reacting for 20-30 min;
(3) adding 10% NaCl solution according to 10% of the crude oil, continuously stirring for 10min, heating to 75-80 deg.C, and removing soap;
(4) after soaping, adding 50% citric acid solution according to 0.05% of the mass of the crude oil, continuously stirring for 30min, and adding 10% NaCl solution according to 10% of the mass of the crude oil, wherein the temperature of the NaCl solution is 80-85 ℃;
(5) oil obtained after NaCl solution is evenly mixed is subjected to oil-water separation and vacuum drying, and the vacuum degree of a dryer is 10-20 mmHg;
(6) heating the drying oil to 100-110 deg.C, vacuum decolorizing for 25-35 min;
(7) heating the decolorized oil to 210-220 ℃, delivering the decolorized oil to a deacidification tower for deacidification, continuously heating the deacidified oil to 235-250 ℃ for deodorization in a plate tower or a packed tower;
(8) and adding 50% citric acid solution into the cooled deodorized oil according to the mass of 0.005% -0.01% of the deodorized oil, quickly mixing, polishing, filtering, and checking to obtain the finished product.
2. The process for refining ultra-high acid value crude oil according to claim 1, wherein: in the step (1), the crude oil with ultrahigh acid value is heated to 50 ℃, 75 percent or 85 percent of phosphoric acid is added according to the amount of 3-4kg of crude oil per ton, and after rapid stirring, the mixture is continuously stirred and reacts for 30-60 min.
3. The process for refining ultra-high acid value crude oil according to claim 1, wherein: and (4) removing the soap in the step (3) by standing precipitation or centrifugation.
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| CN105176676A (en) * | 2015-07-17 | 2015-12-23 | 广州市正德生物科技有限公司 | Edible plant oil non-soap refining method |
| CN105296145A (en) * | 2015-10-13 | 2016-02-03 | 中国林业科学研究院亚热带林业研究所 | Method for processing base oil of tea oil cosmetic |
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2017
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Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101805666A (en) * | 2010-04-02 | 2010-08-18 | 安徽省思润谷物油精炼有限公司 | Process for extracting high-grade rice bran oil by physical method |
| CN102205230A (en) * | 2011-05-14 | 2011-10-05 | 山西大学 | Method for processing atlapulgite for decolorizing grease |
| CN102766532A (en) * | 2012-08-10 | 2012-11-07 | 威县元亨油脂有限公司 | Alkali refining washing process for cottonseed oil |
| CN103409234A (en) * | 2013-08-21 | 2013-11-27 | 南通海辰蛋白科技有限公司 | Process for extracting cottonseed salad oil |
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