CN1569782A - Method for preparing isohexane solvent - Google Patents
Method for preparing isohexane solvent Download PDFInfo
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- CN1569782A CN1569782A CN 200410027004 CN200410027004A CN1569782A CN 1569782 A CN1569782 A CN 1569782A CN 200410027004 CN200410027004 CN 200410027004 CN 200410027004 A CN200410027004 A CN 200410027004A CN 1569782 A CN1569782 A CN 1569782A
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- isohexane
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- solvent
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Abstract
The invention relates to a method for preparing isohexane solvent, wherein No.6 solvent oil is used as the raw material, the distillation is carried out in a filler tower continuously, the isohexane oil distillation fraction at 58-63 deg. C is collected at the bottom of the tower, the unwanted substance is removed in a hydrogenation bank in a continuo's pattern, the hydrogen ratio is 50 : 1.
Description
Technical field
The present invention relates to a kind of manufacture method of petrochemical complex, a kind of more precisely by the manufacture method of extracting, separation means obtains high purity product.
Background technology
The existing phase of history of the application of aromatic solvent in Industrial products period is such as with wide spectrums such as solvents application being arranged all in aerosol industry, coating, rubber industry, binding agent and adhesive agent, sealing agent, plastic material and detergent for precision instrument, dry-cleaning.But after it had caused havoc to environment along with discovery, people had adopted with normal hexane and have replaced, but normal hexane is known from experience the poisoning of generation nervus centralis to the people, is restricted in the use.And isohexane product aromatic free in fact, and normal hexane content is also few, thereby can be not harmful, can not bring destruction to environment yet.So progressively replace by isohexane at above-described wide spectrum.Make the method for isohexane, as Japanese publication communique (A), patent application publication number, among the Te Kaiping 7-242570 " manufacture method of hydrocarbon cosolvent ", the raffinate of preceding operation is adopted the method for fractionation by distillation, promptly the 1st tower separates lightweight part and dissident's alkanes from cat head, distill refining at the 2nd tower and the 3rd tower resulting overhead distillate again, obtain comprising the distillate of the hydrocarbon cosolvent of dissident's alkanes at last, the fractional distillation test result of this distillate, 5% to distillate a little be 60.1 ℃, and 95% to distillate a little be 61 ℃, and describe and the normal hexane amount is arranged below 2%.In the product that the manufacture method of this patent application document record obtains, isohexane is a main component, and normal hexane content is low, is suitable for environmental requirement.But this manufacture method is from " raffinate " back operation, it is distillation process, also need just can finish through three towers, so investment is big, floor space is big, the schedule of operation complexity, maintenance, management workload is big, and this is an one, and it two is this patent application operations after " raffinate ", do not put down in writing any concrete equipment and operational condition, those skilled in the art are to implement this manufacture method by the disclosure file.
Summary of the invention
The manufacture method that the purpose of this invention is to provide a kind of isohexane solvent, its single tower continuity mode of production, less investment, floor space is little, operates, manages simply, the efficient height.
The technology of the present invention solution is achieved like this; The present invention with No. 6 solvent naphthas of the fraction of 60 to 90 ℃ of boiling spreads as raw material; Distillation is 30～35 at tower height degree and diameter ratio all the time: 1; The silk screen of structured filling material layer and the Burden of mellapak packing are 1～1.5 in the tower: carry out continuously in 1 the packed tower; Collect 58～63 ℃ isohexane fraction oil; Continuation mode is after hydrogenation is removed harmful substance in the hydrogenation tank again; Obtain the isohexane of amount more than 95%; And amount is less than 3% n-hexane
Carry out the distillatory manufacturing conditions in single packing tower continuously:
A), No. 6 solvent oil feeding line speed 0.74 meter per seconds;
B), 50～55 ℃ of tower top temperatures, 69～72 ℃ of column bottom temperatures, side stream temperature are 61～65 ℃, the trim the top of column temperature is 40～48 ℃, the trim the top of column ratio is 50～70, the working pressure of tower is 0.105MPa (cutting off);
Operational condition in the hydrogenation jar:
Reaction pressure is 1.0MPa, and temperature of reaction is 150 ℃, and air speed is 2-3h
-1, hydrogen-oil ratio is 50: 1, adopts the continuous production mode.
The above isohexane is for containing 2,2-dimethylbutane, 2,3-dimethylbutane, 2-methylpentane, the summation of 3-methylpentane.
Hydrogenation in the hydrogenation jar of the present invention is optionally to remove unsaturated hydrocarbons.
In the prior art, fractionation isohexane fraction adopts two towers even three tower process flow processs, at first tower lightweight part is steamed from cat head, distillate enters second tower at the bottom of the tower, perhaps method enters the 3rd tower more like this, and overhead distillate obtains the isohexane fraction, and heavy partly distillates at the bottom of tower.And the present invention is condensed to a tower process flow process with two tower process flow processs, and equipment and operational condition are complete, and isohexane distillates from the side line of tower, and lightweight part and heavy partly distillate at the bottom of cat head and tower respectively.Isohexane content of the present invention is more than 95%, and normal hexane content is less than 3%, and aromaticity content is less than 50PPM, and sulphur content does not contain unsaturated hydrocarbons substantially less than 5PPM.
The isohexane solvent that the inventive method makes is the replace solvents of normal hexane, to environment, human body safety, can not produce the destructive influence, so Application Areas is extensive, also can replace in all Application Areass of normal hexane.
The beneficial effect that manufacture method of the present invention obtains is, its single tower continuity mode of production, and less investment, floor space is little, operates, manages simply, the efficient height.
Embodiment
As raw material, distillation is 33: 1 at tower height degree and diameter ratio all the time with No. 6 solvent oils of the fraction of 60 to 90 ℃ of boiling spreads in the present invention, and the Stainless Steel Cloth of the interior structured filling material layer of tower is 1.3 with the collocation ratio of Mellapak packing; Carry out continuously in 1 the packing tower, collect 58～63 ℃ isohexane fraction oil, continuous mode obtains the isohexane of amount more than 95% after hydrogenation is removed unsaturated hydrocarbons in the hydrogenation jar again, and amount is less than 3% normal hexane,
Carry out the distillatory manufacturing conditions in single packing tower continuously:
A), No. 6 solvent oil feeding line speed 0.74 meter per seconds;
B), 53 ℃ of tower top temperatures, 70 ℃ of column bottom temperatures, 63 ℃ of side stream temperatures, the trim the top of column temperature is 45 ℃; The trim the top of column ratio is 60, and the working pressure of tower is 0.105MPa (cutting off);
Operational condition in the hydrogenation jar:
Reaction pressure is 1.0MPa, and temperature of reaction is 150 ℃, and air speed is 2-3h
-1, hydrogen-oil ratio is 50: 1, adopts the continuous production mode.
The isohexane solvent of indication of the present invention is to contain 2,2-dimethylbutane, 2,3-dimethylbutane, 2-methylpentane, the summation of 3-methylpentane.
Claims (3)
1, the manufacture method of isohexane solvent, it is characterized in that No. 6 solvent oils with the fraction of 60 to 90 ℃ of boiling spreads are as raw material, collect 58～63 ℃ isohexane fraction oil, continuous mode is after hydrogenation is removed objectionable impurities in the hydrogenation jar again, obtain the isohexane of amount more than 95%, and amount carries out the distillatory manufacturing conditions continuously less than 3% normal hexane in single packing tower:
Distillation is 30～35 at tower height degree and diameter ratio all the time: 1
The silk screen of structured filling material layer is 1～1.5 with the collocation ratio of Mellapak packing in the tower: carry out continuously in 1 the packing tower,
A), No. 6 solvent oil feeding line speed 0.74 meter per seconds;
B), 50～55 ℃ of tower top temperatures, 69～72 ℃ of column bottom temperatures, 61～65 ℃ of side stream temperatures, the trim the top of column temperature is 40～48 ℃, the trim the top of column ratio is 50～70;
Operational condition in the hydrogenation jar:
Reaction pressure is 1.0MPa, and temperature of reaction is 150 ℃, and air speed is 2-3h-1, and hydrogen-oil ratio is 50: 1, adopts the continuous production mode.
2, the manufacture method of isohexane solvent according to claim 1 is characterized in that described isohexane is for containing 2,2-dimethylbutane, 2,3-dimethylbutane, 2-methylpentane, the summation of 3-methylpentane.
3, the manufacture method of isohexane solvent according to claim 1 is characterized in that hydrogenation in the hydrogenation jar, optionally removes unsaturated hydrocarbons.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410027004 CN1238313C (en) | 2004-04-27 | 2004-04-27 | Method for preparing isohexane solvent |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410027004 CN1238313C (en) | 2004-04-27 | 2004-04-27 | Method for preparing isohexane solvent |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1569782A true CN1569782A (en) | 2005-01-26 |
| CN1238313C CN1238313C (en) | 2006-01-25 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200410027004 Expired - Fee Related CN1238313C (en) | 2004-04-27 | 2004-04-27 | Method for preparing isohexane solvent |
Country Status (1)
| Country | Link |
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| CN (1) | CN1238313C (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101200405B (en) * | 2007-11-22 | 2010-05-19 | 广州赫尔普化工有限公司 | Method for manufacturing hexane solvent oil |
| CN102180759A (en) * | 2011-03-23 | 2011-09-14 | 北京燕山集联石油化工有限公司 | Method for preparing hexane |
| CN102212392A (en) * | 2011-05-10 | 2011-10-12 | 广州赫尔普化工有限公司 | Preparation method of edible oil leaching agent |
| CN102675023A (en) * | 2012-05-19 | 2012-09-19 | 淄博汇佳橡胶新型材料有限公司 | Preparation method of narrow-fraction high-purity isohexane |
| CN103073383A (en) * | 2013-02-07 | 2013-05-01 | 天津大学 | Method and device for separating isohexane, n-hexane and benzene |
| CN101875594B (en) * | 2009-04-30 | 2013-12-11 | 中国海洋石油总公司 | Method for preparing narrow fraction nontoxic high-purity isohexane |
| CN103833499A (en) * | 2012-11-27 | 2014-06-04 | 中国石油天然气股份有限公司 | Method for preparing high-purity isohexane solvent oil |
| 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 |
| CN108114499A (en) * | 2018-01-22 | 2018-06-05 | 广州赫尔普化工有限公司 | A kind of environment-friendly light alkane production system and the production method using the production system |
-
2004
- 2004-04-27 CN CN 200410027004 patent/CN1238313C/en not_active Expired - Fee Related
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101200405B (en) * | 2007-11-22 | 2010-05-19 | 广州赫尔普化工有限公司 | Method for manufacturing hexane solvent oil |
| CN101875594B (en) * | 2009-04-30 | 2013-12-11 | 中国海洋石油总公司 | Method for preparing narrow fraction nontoxic high-purity isohexane |
| CN102180759A (en) * | 2011-03-23 | 2011-09-14 | 北京燕山集联石油化工有限公司 | Method for preparing hexane |
| CN102180759B (en) * | 2011-03-23 | 2013-07-31 | 北京燕山集联石油化工有限公司 | Method for preparing hexane |
| CN102212392B (en) * | 2011-05-10 | 2013-11-20 | 广州赫尔普化工有限公司 | Preparation method of edible oil leaching agent |
| CN102212392A (en) * | 2011-05-10 | 2011-10-12 | 广州赫尔普化工有限公司 | Preparation method of edible oil leaching agent |
| CN102675023A (en) * | 2012-05-19 | 2012-09-19 | 淄博汇佳橡胶新型材料有限公司 | Preparation method of narrow-fraction high-purity isohexane |
| CN102675023B (en) * | 2012-05-19 | 2014-08-27 | 淄博汇佳橡胶新型材料有限公司 | Preparation method of narrow-fraction high-purity isohexane |
| CN103833499A (en) * | 2012-11-27 | 2014-06-04 | 中国石油天然气股份有限公司 | Method for preparing high-purity isohexane solvent oil |
| CN103833499B (en) * | 2012-11-27 | 2016-03-09 | 中国石油天然气股份有限公司 | A kind of preparation method of high purity isohexane solvent oil |
| CN103073383A (en) * | 2013-02-07 | 2013-05-01 | 天津大学 | Method and device for separating isohexane, n-hexane and benzene |
| 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 |
| CN108114499A (en) * | 2018-01-22 | 2018-06-05 | 广州赫尔普化工有限公司 | A kind of environment-friendly light alkane production system and the production method using the production system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1238313C (en) | 2006-01-25 |
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Granted publication date: 20060125 Termination date: 20140427 |