CN102212392B - Preparation method of edible oil leaching agent - Google Patents
Preparation method of edible oil leaching agent Download PDFInfo
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- CN102212392B CN102212392B CN2011101197117A CN201110119711A CN102212392B CN 102212392 B CN102212392 B CN 102212392B CN 2011101197117 A CN2011101197117 A CN 2011101197117A CN 201110119711 A CN201110119711 A CN 201110119711A CN 102212392 B CN102212392 B CN 102212392B
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Abstract
The invention relates to a preparation method of an edible oil leaching agent, in particular to a preparation method of the leaching agent used in edible oil industries; and the preparation method comprises the following steps of: taking aromatic raffinate oil refined by petroleum as a raw material, and by using a fibrous membrane contactor, carrying out washing and desulfuration, dehydration, hydrogenation deolefination, hydrogenation dearomatization, distillation and the like so as to obtain the leaching agent with high quality. The preparation method has the advantages of increasing the product quality and recovery rate of a solvent, decreasing residual oil in oil residuals, reducing the solvent loss and energy consumption, being beneficial to increasing the quality of oil and oil residuals, having no influence on environments and being safe to human bodies.
Description
Technical field
The present invention relates to a kind of manufacture method of the leaching agent that petrochemical complex and mankind's edible oil industry use.
Background technology
The mankind's food oils will extract from oilseed plant, way the earliest is to adopt milling process to extract, and, for improving oil yield, gradually adopts lixiviation process.The extraction that develops into present most vegetables oil has been to utilize solvent extraction---lixiviation process.
China produces more than 2,000 ten thousand tons of edible oils at present per year,, by the estimation of industry formula, will consume the edible oil extraction solvent of more than 100,000 ton minimum every year; The leaching process of food oils, at first will use the oil plants such as leaching agent Jin bubble Da Dou ﹑ peanut, and then the crude oil that leaches is processed into the edible oil of various kind grades, and leaching solvent is essential to extracting the edible oil operation.To industrial environment and improving constantly of pollute requiring thereof, people also require more and more higher, certainly, just higher to the specification of quality of edible oil leaching agent to the quality of edible oil along with society.At first be that requirement to boiling range is that the boiling range scope is more and more narrow, besides the content of harmful material such as Ben ﹑ alkene and sulphur etc. control require more and more stricter.60～90 ℃ of the vegetable oil extraction solvent boiling ranges of past use, aromaticity content is less than 1%, and bromine index is not more than 1000mgBr/100g, extraction solvent second-rate, in edible oil, the risk of residual harmful substance is higher.For this reason, the new edible oil leaching agent of social needs research and development solves public's requirement more and more higher to food safety, and country has issued new vegetable oil extraction solvent standard.Its leading indicator benzene content is less than 1000PPM, and bromine index is not more than 100mgBr/100g(and does not substantially contain alkene), sulphur content is less than 5PPM, 61～76 ℃ of boiling range scopes.This standard does not reach the world level requirement of food service industry yet.
The present invention develops a kind of new manufacture method and produces the leaching agent that reaches edible oil industry world level specification of quality, to meet edible oil industry user's needs.Such as, benzene content is less than 50PPM, bromine index is not more than 5mgBr/100g(and does not substantially contain alkene), sulphur content is less than 0.5PPM, 66～70 ℃ of boiling range scopes.
Summary of the invention
The manufacture method that the purpose of this invention is to provide a kind of edible oil leaching agent.The quality product that adopts the method to produce is high, and in oily Hectometer, Residual oil descends, and solvent recovering rate is high, and solvent loss reduces, and energy consumption descends.
The technology of the present invention solution is achieved like this.It is that a kind of aromatic hydrocarbons take refining of petroleum is raffinated oil as raw material, by raw material being carried out desulfurization, dehydration, hydrogenation and olefin hydrocarbon removal and taking off the means such as aromatic hydrocarbons, precision fractional distillation, obtains the manufacture method of high-quality edible oil leaching agent.
The aromatic hydrocarbons of the above refining of petroleum is raffinated oil and is entered fiber-film contact, operational condition is that oil-water ratio is by 10:2 ~ 4, service temperature is 40 ℃, working pressure 0.1 ~ 1.0MPa, the fiber-film contact pressure drop is less than 0.07 MPa, removing moisture from fiber-film contact oil phase out through the molecular sieve facility, its water-content is controlled less than 100PPM.
Of the present invention with desulfurization, the dehydration after raw material enter hydrogenator, reaction pressure is 1.0 ~ 2.5MPa, temperature of reaction is 150 ℃, air speed is 2-3h
-1, hydrogen-oil ratio is 50:1.
Of the present invention hydrogenated oil is entered the precision fractional distillation tower, the ratio in the high footpath of its tower is 40:1, it is silk screen and the Mellapak packing of the structured filling material layer of 1.5:1 that column internals adopts Burden, feeding temperature is 40 ℃, and tower top temperature is 55 ~ 60 ℃, and column bottom temperature is 72 ~ 78 ℃, side stream temperature is 65 ~ 70 ℃, the trim the top of column temperature is 40～48 ℃, and the trim the top of column ratio is 50～70, and the working pressure of tower is that 0.105MPa(is exhausted).
Aromatic hydrocarbons of the present invention is raffinated oil and is referred in petroleum refining process, be rich in aromatic hydrocarbons C6 ~ C8 component with extraction (extracting) aromatic hydrocarbons after remaining distillate, its main component is the alkane of C6 ~ C8 and a certain amount of naphthenic hydrocarbon and contains a small amount of aromatic hydrocarbons.
The present invention raffinates oil as raw material take the aromatic hydrocarbons of refining of petroleum, by raw material being carried out desulfurization, dehydration, hydrogenation and olefin hydrocarbon removal and taking off the means such as aromatic hydrocarbons, precision fractional distillation, obtains the manufacture method of the leaching agent that high-quality edible oil industries use.
Owing to containing a small amount of sulphur (50 ~ 100PPM) in raw material, it is mainly the tetramethylene sulfone (extraction solvent) of carrying secretly in aromatics extraction process, the characteristics of utilizing tetramethylene sulfone and water to dissolve each other, adopt softening water to wash and tetramethylene sulfone is removed (sulphur content is less than 0.5PPM) by fiber-film contact, then through the molecular sieve dehydration facility, remove moisture (water-content is less than 100PPM).
Fiber-film contact is a kind of Static Contact equipment, formed by the long and continuous minor diameter of a branch of bundle (Ф 1.0MM) fiber yarn, wrap in the container of a pipe or other cylinder shape, so that effectively the enough fiberfill fibers of cross section, to provide, the required a large amount of surface-area of mass transfer occurs.Tetramethylene sulfone in by the water treatment soln with effect of mass transmitting, aromatic hydrocarbons being raffinated oil is removed---and the tetramethylene sulfone during aromatic hydrocarbons is raffinated oil is transferred in the aqueous solution, the aqueous solution flows to the separating tank bottom, and oil product flows out (fiber-film contact is successful Application on Alkali cleaning of gasoline mercaptan removal and oil liquefied gas caustic wash desulfuration hydrogen production device) from the top of separating tank.
The beneficial effect that manufacture method of the present invention obtains is to adopt different technological processs to mutually combine, and the high-quality edible oil leaching agent of consecutive production, compare and have the high characteristics of quality product (seeing attached list) with analogous products (vegetable oil extraction solvent), in product, active principle normal hexane content is up to more than 70%, boiling range narrow range (66～70 ℃), benzene content low (less than 50PPM), sulphur content is controlled at below 0.5PPM, bromine index is not more than 5mgBr/100g, and quality product is reached advanced world standards higher than national standard.
The edible oil leaching agent that the inventive method makes,, to environment, human-body safety, can not produce the impact on environmental disruption, therefore in edible oil industry (extraction solvent), is used widely.
The quality contrast of subordinate list edible oil leaching agent and vegetable oil extraction solvent
Embodiment
The present invention is undertaken by following program:
1, the aromatic hydrocarbons of refining of petroleum raffinate oil (its main component is the alkane of C6～C8 and a certain amount of naphthenic hydrocarbon and contains a small amount of aromatic hydrocarbons) enter fiber-film contact, remove sulphur by the washing Arene removal tetramethylene sulfone that carries of raffinating oil, operational condition is that oil-water ratio is by 10:2 ~ 4, service temperature is 40 ℃, working pressure 0.1 ~ 1.0MPa, the fiber-film contact pressure drop is less than 0.07 MPa.Removing moisture from fiber-film contact oil phase out through the molecular sieve facility, thereby reaching the purpose that removes sulphur, its water-content is controlled less than 100PPM.
2, the raw material after desulfurization, dehydration is entered hydrogenator, reaction pressure is 1.0 ~ 2.5MPa, and temperature of reaction is 150 ℃, and air speed is 2-3h
-1, hydrogen-oil ratio is 50:1.
3, hydrogenated oil enters the precision fractional distillation tower, the ratio in the high footpath of its tower is 40:1, it is silk screen and the Mellapak packing of the structured filling material layer of 1.5:1 that column internals adopts Burden, feeding temperature is 40 ℃, and tower top temperature is 55 ~ 60 ℃, and column bottom temperature is 72 ~ 78 ℃, side stream temperature is 65 ~ 70 ℃, the trim the top of column temperature is 40～48 ℃, and the trim the top of column ratio is 50～70, and the working pressure of tower is that 0.105MPa(is exhausted).
4, from precision fractional distillation tower edible oil leaching agent out, 66～70 ℃ of boiling range scopes, aromaticity content is less than 50 PPM, and sulphur content is less than 0.5PPM, and bromine index is less than 5 mgBr/100g.
Claims (1)
1. the manufacture method of an edible oil leaching agent, raffinate oil as raw material take the aromatic hydrocarbons of refining of petroleum, it is characterized in that comprising the steps:
(1) aromatic hydrocarbons of refining of petroleum is raffinated oil and is entered fiber-film contact, the sulphur of by washing Arene removal, raffinating oil and carrying, operational condition is that oil-water ratio is by 10:2 ~ 4, service temperature is 40 ℃, working pressure 0.1 ~ 1.0MPa, the fiber-film contact pressure drop, less than 0.07 MPa, removes moisture through the molecular sieve facility again from fiber-film contact oil phase out, thereby reach the purpose that removes sulphur, its water-content is controlled less than 100PPM;
(2) raw material after desulfurization, dehydration is entered hydrogenator, reaction pressure is 1.0 ~ 2.5MPa, and temperature of reaction is 150 ℃, and air speed is 2-3h
-1, hydrogen-oil ratio is 50:1;
(3) hydrogenated oil enters the precision fractional distillation tower, the ratio in the high footpath of its tower is 40:1, it is silk screen and the Mellapak packing of the structured filling material layer of 1.5:1 that column internals adopts Burden, feeding temperature is 40 ℃, and tower top temperature is 55 ~ 60 ℃, and column bottom temperature is 72 ~ 78 ℃, side stream temperature is 65 ~ 70 ℃, the trim the top of column temperature is 40～48 ℃, and the trim the top of column ratio is 50～70, and the working pressure of tower is 0.105MPa;
(4) from precision fractional distillation tower edible oil leaching agent out, 66～70 ℃ of boiling range scopes, aromaticity content is less than 50 PPM, and sulphur content is less than 0.5PPM, and bromine index is less than 5 mgBr/100g.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2011101197117A CN102212392B (en) | 2011-05-10 | 2011-05-10 | Preparation method of edible oil leaching agent |
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| CN2011101197117A CN102212392B (en) | 2011-05-10 | 2011-05-10 | Preparation method of edible oil leaching agent |
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| CN102212392A CN102212392A (en) | 2011-10-12 |
| CN102212392B true CN102212392B (en) | 2013-11-20 |
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| CN106311194A (en) * | 2015-07-06 | 2017-01-11 | 中国石油化工股份有限公司 | Hydrogenation catalyst for producing extracted oil of edible oil as well as preparation method and application thereof |
| CN108048133B (en) * | 2017-12-08 | 2020-04-07 | 广州赫尔普化工有限公司 | Method for joint production of n-hexane and clean gasoline blending component |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1569782A (en) * | 2004-04-27 | 2005-01-26 | 广州赫尔普化工有限公司 | Method for preparing isohexane solvent |
| CN101875854A (en) * | 2009-04-30 | 2010-11-03 | 中国海洋石油总公司 | Method for preparing narrow fraction low-aromatic hydrocarbon No.6 solvent oil |
| CN101974347A (en) * | 2010-09-17 | 2011-02-16 | 天津精华石化有限公司 | Process for producing solvent oil by removing aromatic hydrocarbon from raffinate oil |
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2011
- 2011-05-10 CN CN2011101197117A patent/CN102212392B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1569782A (en) * | 2004-04-27 | 2005-01-26 | 广州赫尔普化工有限公司 | Method for preparing isohexane solvent |
| CN101875854A (en) * | 2009-04-30 | 2010-11-03 | 中国海洋石油总公司 | Method for preparing narrow fraction low-aromatic hydrocarbon No.6 solvent oil |
| CN101974347A (en) * | 2010-09-17 | 2011-02-16 | 天津精华石化有限公司 | Process for producing solvent oil by removing aromatic hydrocarbon from raffinate oil |
Non-Patent Citations (1)
| Title |
|---|
| 刘振宁等.纤维膜脱硫技术在RFCC汽油脱臭单元的应用.《石油炼制与化工》.2002, * |
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