CN102212392A - Preparation method of edible oil leaching agent - Google Patents
Preparation method of edible oil leaching agent Download PDFInfo
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- CN102212392A CN102212392A CN2011101197117A CN201110119711A CN102212392A CN 102212392 A CN102212392 A CN 102212392A CN 2011101197117 A CN2011101197117 A CN 2011101197117A CN 201110119711 A CN201110119711 A CN 201110119711A CN 102212392 A CN102212392 A CN 102212392A
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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 human edible oil industry use.
Background technology
Human food oils will extract from oilseed plant, and 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 prescription, will consume more than 100,000 ton edible oil extraction solvent minimum every year; The leaching process of food oils at first will use 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 it is essential to extracting the edible oil operation to leach solvent.Along with society 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.At first be that requirement to boiling range is that the boiling range scope is more and more narrow, the content control of harmful besides material such as Ben ﹑ alkene and sulphur etc. requires more and more stricter.60～90 ℃ of the vegetables oil extraction solvent boiling ranges of past usefulness, aromaticity content is less than 1%, and bromine index is not more than 1000mgBr/100g, extraction solvent second-rate, the risk of residual harmful substance is higher in the edible oil.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 vegetables 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 contain alkene substantially), 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 satisfy 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 contain alkene substantially), 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 height that adopts this method to produce, Residual oil descends among the oily Hectometer, the solvent recovering rate height, 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 with refining of petroleum raffinates oil is raw material, by raw material being carried out desulfurization, dehydration, hydrogenation and olefin hydrocarbon removal and taking off the manufacture method that means such as aromatic hydrocarbons, precision fractional distillation obtain high-quality edible oil leaching agent.
The aromatic hydrocarbons of the above refining of petroleum is raffinated oil and is entered the tunica fibrosa contactor, operational condition is that oil-water ratio is by 10:2 ~ 4, service temperature is 40 ℃, working pressure 0.1 ~ 1.0MPa, the pressure drop of tunica fibrosa contactor is less than 0.07 MPa, the oil phase that comes out from the tunica fibrosa contactor is removing moisture through the molecular sieve facility, and its water-content control is less than 100PPM.
Of the present invention desulfurization, dehydrated raw material are 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.
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, column internals adopts collocation than the silk screen and the Mellapak packing that are the structured filling material layer of 1.5:1, 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 meant in the 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 spot of aromatic hydrocarbons.
The present invention is that to raffinate oil with the aromatic hydrocarbons of refining of petroleum be raw material, by raw material being carried out desulfurization, dehydration, hydrogenation and olefin hydrocarbon removal and taking off the manufacture method that means such as aromatic hydrocarbons, precision fractional distillation obtain the leaching agent that high-quality edible oil industries use.
Owing to contain a spot of sulphur (50 ~ 100PPM) in the raw material, it mainly is the tetramethylene sulfone of carrying secretly in the aromatics extraction process (extraction solvent), the characteristics of utilizing tetramethylene sulfone and water to dissolve each other, adopt softening water tetramethylene sulfone to be removed (sulphur content is less than 0.5PPM), remove moisture (water-content is less than 100PPM) through the molecular sieve dehydration facility again by the washing of tunica fibrosa contactor.
The tunica fibrosa contactor is a kind of Static Contact equipment, successive minor diameter (Ф 1.0MM) fiber yarn is formed by a branch of bundle is long, 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 take place.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 (the tunica fibrosa contactor is successful Application on the pure and mild oil liquefied gas caustic wash desulfuration of gasoline 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 continuity is produced high-quality edible oil leaching agent, compare with analogous products (vegetables oil extraction solvent) and to have the high characteristics of quality product (seeing attached list), active principle normal hexane content is up to more than 70% in the product, boiling range narrow range (66～70 ℃), benzene content low (less than 50PPM), sulphur content is controlled at below the 0.5PPM, bromine index is not more than 5mgBr/100g, and quality product is higher than national standard and reaches advanced world standards.
The edible oil leaching agent that the inventive method makes to environment, human body safety, can not produce the influence to environmental disruption, therefore is used widely in edible oil industry (extraction solvent).
The quality contrast of subordinate list edible oil leaching agent and vegetables 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 spot of aromatic hydrocarbons) enter the tunica fibrosa contactor, remove the aromatic hydrocarbons tetramethylene sulfone that carries of raffinating oil by water elution and remove sulphur, operational condition is that oil-water ratio is by 10:2 ~ 4, service temperature is 40 ℃, working pressure 0.1 ~ 1.0MPa, the pressure drop of tunica fibrosa contactor is less than 0.07 MPa.The oil phase that comes out from the tunica fibrosa contactor is removing moisture through the molecular sieve facility, thereby reaches the purpose that removes sulphur, and its water-content control is less than 100PPM.
2, desulfurization, dehydrated raw material are 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, column internals adopts collocation than the silk screen and the Mellapak packing that are the structured filling material layer of 1.5:1, 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, the edible oil leaching agent that comes out from the precision fractional distillation tower, 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 (4)
1. the manufacture method of an edible oil leaching agent is characterized in that it is raw material that a kind of aromatic hydrocarbons with refining of petroleum is raffinated oil, and obtains the manufacture method of the leaching agent that the edible oil industry uses by means such as desulfurization, dehydration, hydrogenation and olefin hydrocarbon removal and hydrogenation aromatics-removing, distillations.
2. the manufacture method of a kind of edible oil leaching agent according to claim 1, it is characterized in that raffinating oil with the aromatic hydrocarbons of refining of petroleum is raw material, enter the tunica fibrosa contactor, remove the tetramethylene sulfone that aromatic hydrocarbons is raffinated oil and carried by water elution, operational condition is that oil-water ratio is by 10:2 ~ 4, service temperature is 40 ℃, working pressure 0.1 ~ 1.0MPa, the pressure drop of tunica fibrosa contactor is less than 0.07 MPa, the oil phase that comes out from the tunica fibrosa contactor is removing moisture through the molecular sieve facility, thereby reach the purpose that removes sulphur, its water-content control is less than 100PPM.
3. the manufacture method of a kind of edible oil leaching agent according to claim 1 is characterized in that desulfurization, dehydrated raw material are entered hydrogenator, and 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.
4. the manufacture method of a kind of edible oil leaching agent according to claim 1, it is characterized in that hydrogenated oil enters the precision fractional distillation tower, the ratio in the high footpath of its tower is 40:1, column internals adopts collocation than the silk screen and the Mellapak packing that are the structured filling material layer of 1.5:1, feeding temperature is 40 ℃, tower top temperature is 55～60 ℃, column bottom temperature is 72～78 ℃, side stream temperature is 65～70 ℃, the trim the top of column temperature is 40～48 ℃, the trim the top of column ratio is 50～70, and the operation absolute pressure of tower is 0.105MPa.
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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 true CN102212392A (en) | 2011-10-12 |
| CN102212392B CN102212392B (en) | 2013-11-20 |
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| CN2011101197117A Expired - Fee Related CN102212392B (en) | 2011-05-10 | 2011-05-10 | Preparation method of edible oil leaching agent |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN108048133A (en) * | 2017-12-08 | 2018-05-18 | 广州赫尔普化工有限公司 | A kind of method of Joint Production n-hexane and clean gasoline blend component |
Citations (3)
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| 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 |
-
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》 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN108048133A (en) * | 2017-12-08 | 2018-05-18 | 广州赫尔普化工有限公司 | A kind of method of Joint Production n-hexane and clean gasoline blend component |
| 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 |
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| CN102212392B (en) | 2013-11-20 |
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Effective date of registration: 20131211 Address after: 510726 No. 170, Whampoa Petrochemical Road, Guangdong, Guangzhou Patentee after: GUANGZHOU HIRP CHEMICAL Co.,Ltd. Address before: 510726 No. 170, Whampoa Petrochemical Road, Guangdong, Guangzhou Patentee before: GUANGZHOU HIRP CHEMICAL Co.,Ltd. Patentee before: Guangzhou Kindwood Co.,Ltd. |
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Granted publication date: 20131120 |