CN101289362B - Process for preparing 1-amylene by separating C5 distillate of petroleum - Google Patents
Process for preparing 1-amylene by separating C5 distillate of petroleum Download PDFInfo
- Publication number
- CN101289362B CN101289362B CN200710039674A CN200710039674A CN101289362B CN 101289362 B CN101289362 B CN 101289362B CN 200710039674 A CN200710039674 A CN 200710039674A CN 200710039674 A CN200710039674 A CN 200710039674A CN 101289362 B CN101289362 B CN 101289362B
- Authority
- CN
- China
- Prior art keywords
- amylene
- temperature
- tower still
- tower
- distillate
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a method which is used for preparing 1-pentene by separating petroleum C5 fraction and takes raffinate C5 obtained after separating diolefin and isoamylene by extracting as raw materials. The process comprises that the raw materials are extracted and distilled, and the extractant is N and N-dimethylformamide, the feeding weight ratio of the raw materials and the extractantis 1:5 to 1:12, C5 saturated hydrocarbon materials are discharged from a column top, and the materials richly containing 1-pentene and the extractant are obtained in a column bottom; the materials inthe column bottom obtained in the process 1 are distilled so as to recycle the extractant, the materials richly containing 1-pentene are obtained in the column top, the extractant is obtained in the column bottom, and the extractant can be recycled; the materials in the column top obtained in the process 2 are distilled and separated so as to remove heavy components, the crude product of 1-pentene are obtained from the column top, and the materials with heavy components are discharged from the column bottom; and the crude product of 1-pentene obtained in the process 3 is distilled and refinedso as to remove light components, the materials in the column bottom are taken and a refined product of 1-pentene is obtained. By processing at a much deeper degree, the method of the invention solves a technical problem that 1-pentene in C5 fraction can not be utilized by the prior art.
Description
Technical field
The present invention relates to the separation method of Petrocarbon 5 distillate, particularly separate the method for producing the 1-amylene by the Petrocarbon 5 distillate through technological processs such as rectifying, extracting rectifyings.
Background technology
The a considerable amount of C5 fractions of process by-product of petroleum cracking system ethene, its amount is about 10% of ethylene yield, is the effective way that improves the ethylene production economic benefit to the comprehensive utilization of C5 fraction.The comprehensive utilization of C5 fraction at present mainly is extracting to be carried out in C5 fraction separate, and obtains being worth diolefin and isopentene such as higher m-pentadiene, isoprene and NSC 7352.Separate the surplus Petrocarbon 5 distillate of taking out of diolefin and isopentene material through extracting and accounted for 10～15% of C5 fraction raw material.The component boiling point of taking out surplus Petrocarbon 5 distillate is very approaching, its separation difficulty, and the oil that generally only acts as a fuel uses.Take out surplus Petrocarbon 5 distillate material for this, existing deep processing and utilization is the mixture that obtains pentane and iso-pentane through full hydrogenation, is introduced like Chinese patent ZL02145057.9, ZL02145056.0.The mixture of pentane, pentane and iso-pentane can be used as whipping agent, extraction agent, green refrigerant and organic solvent etc., and this method has further improved the utility value of taking out surplus Petrocarbon 5 distillate.But; In fact take out and contain 30～40% the amylene of having an appointment in the surplus Petrocarbon 5 distillate material and (comprise 1-amylene and 2-amylene; Both ratios are about 1: 2); And the amylene higher industrial chemicals that is using value is synthetic, the medicine synthetic important monomer of polymer modification and complicated organometallics like the 1-amylene, and its price is also far above pentane and iso-pentane.The defective of full hydrogenation technique is to make that amylene can't obtain utilizing.
Summary of the invention
The invention provides and a kind ofly separate the method produce the 1-amylene by the Petrocarbon 5 distillate, it can't utilize this technical problem of 1-amylene in the C5 fraction through the oil C5 fraction being carried out the more processing of the degree of depth to solve prior art.
Below be the detailed technical scheme of the present invention:
A kind ofly separate the method produce the 1-amylene by the Petrocarbon 5 distillate, this method is a raw material with the surplus Petrocarbon 5 distillate of taking out that extracting has separated behind diolefin and the isopentene, and its process comprises:
1) raw material carries out extracting rectifying, and extraction agent is N, dinethylformamide; Raw material is 1: 5～1: 12 with the feed weight ratio of extraction agent, and the extractant feed temperature is 20～45 ℃, and tower top temperature is 25～36 ℃; Tower still temperature is 60～120 ℃, and working pressure is a normal pressure, and reflux ratio is 1～6; Cat head is discharged carbon five stable hydrocarbon materials, and the tower still gets the material of enrichment amylene-1 and extraction agent;
2) process 1) tower still material carry out rectifying to reclaim extraction agent, tower top temperature is 26～32 ℃, tower still temperature is 110～150 ℃; Working pressure is a normal pressure, and reflux ratio is 1～6, and cat head gets the material of enrichment 1-amylene; The tower still gets extraction agent, the extraction agent recycled;
3) process 2) the cat head material carry out rectifying separation to remove heavy constituent, tower top temperature is 26～32 ℃, tower still temperature is 35～45 ℃, working pressure is a normal pressure, reflux ratio is 20～50, gets the thick product of 1-amylene by cat head, the tower still is discharged the heavy constituent material;
4) process 3) the thick product of 1-amylene that obtains carries out that rectified purified tower top temperature is 25～29 ℃ to remove light constituent, and tower still temperature is 35～45 ℃; Working pressure is a normal pressure; Reflux ratio is 20～50, and cat head is discharged the light constituent material, gets tower still material and gets 1-amylene refined prod.
Said process 1) described raw material be preferably 1: 6 with the feed weight ratio of extraction agent～1: 10, the extractant feed temperature is preferably 30～40 ℃, tower still temperature is preferably 65～100 ℃, reflux ratio is preferably 1～4;
Process 2) described tower top temperature is preferably 27～30 ℃, and tower still temperature is preferably 120～140 ℃, and reflux ratio is preferably 1～4;
Process 3) described tower top temperature is preferably 27～30 ℃, and tower still temperature is preferably 38～42 ℃, and reflux ratio is preferably 30～40;
Process 4) described tower still temperature is preferably 38～42 ℃, and reflux ratio is preferably 30～40.
Key of the present invention is to have selected a kind of suitable technology, from take out surplus Petrocarbon 5 distillate, to isolate 1-amylene product effectively.Whole technological process mainly comprises four parts, wherein:
Process 1) purpose is the saturated alkane of removing in the raw material material, is mainly iso-pentane.Because iso-pentane is difficult to separate with the 1-amylene with the method for rectifying, adopt extracting rectifying.Process 1) key is selection of Extractant and Selection of technological conditions.Extractive distillation column can adopt packing tower, and theoretical plate number is advisable with 30～60.The same with most of extraction rectification techniques, extraction agent is preferably by the top charging of tower, and material preferably by in the stripping section near the position charging of tower still.
Process 2) is simple rectifying, its objective is and realize separating of extraction agent and carbon five materials,, can realize both separation fully through simple rectifying once the step because both atmospheric boiling point differences are bigger.The extraction agent that reclaims can return the abstraction distillation system recycled.Rectifying tower can adopt packing tower, and theoretical plate number is advisable with 15～30, material preferably by in the stripping section near the position charging of tower still.
Process 3) purpose is a removal process 2) heavy constituent in the cat head material, mainly comprise Skellysolve A, 2-amylene and a spot of isopentene.The atmospheric boiling point of these heavy constituent materials and 1-amylene are also comparatively approaching, so adopt precise distillation.Rectifying tower can adopt packing tower, and theoretical plate number is at least 40, generally can be no more than 100, is advisable with 40～80, and it is comparatively suitable near the position of tower still that the material feeding mouth is arranged in stripping section.
Process 4) being precise distillation also, its objective is process 3) the thick product of 1-amylene that obtains makes with extra care, and isolates light constituent impurity.Rectifying tower can adopt packing tower, and theoretical plate number is at least 40, generally can be no more than 100, is advisable with 40～80, and it is comparatively suitable near the position of tower still that the material feeding mouth is arranged in stripping section.
Positive effect of the present invention is to take out through further raising the working depth of surplus Petrocarbon 5 distillate material, has obtained higher carbon five products of economic worth, and the more perfect comprehensive utilization means of C 5 fraction are exhausted the waste that has reduced petroleum resources possibly.
Below further describe details of the present invention through concrete embodiment.Being defined as of 1-amylene product yield among the embodiment:
The surplus Petrocarbon 5 distillate raw material composition of taking out that each embodiment uses is seen table 1,
Table 1.
| Component | Content (weight %) |
| The 1-amylene | 17.5 |
| The 2-amylene | 28.6 |
| Skellysolve A | 42.1 |
| Iso-pentane | 5.5 |
| Isopentene | 4.3 |
| 1, the 4-pentadiene | 1.3 |
| Materials such as other hydro carbons | Surplus |
Embodiment
[embodiment 1～10]
Separate by following process like the listed surplus Petrocarbon 5 distillate raw material of taking out of table 1 forming:
1) raw material carries out extracting rectifying, and extraction agent is N, dinethylformamide.Extractive distillation column is a packing tower, and theoretical plate number is 40, and material is by the position charging of the 32nd column plate, and extraction agent is by the position charging of the 4th column plate, and material feeding speed is 1.0kg/h.Working pressure is a normal pressure, and other rectification process condition sees that table 2 is listed.Cat head is discharged carbon five stable hydrocarbon materials, and the tower still gets the material of enrichment 1-amylene and extraction agent;
2) process 1) tower still material carry out rectifying to reclaim extraction agent, rectifying tower is a packing tower, theoretical plate number is 20, raw material is by the position charging of the 16th column plate.Working pressure is a normal pressure, and other extraction rectification technique condition sees that table 3 is listed.Cat head gets the material of enrichment 1-amylene, and the tower still gets extraction agent, and extraction agent returns the abstraction distillation system recycled;
3) process 2) the cat head material carry out rectifying separation to remove heavy constituent, rectifying tower is a packing tower, theoretical plate number is 50, raw material is by the position charging of the 40th column plate, working pressure is a normal pressure, other rectification process condition sees that table 4 is listed.Get the thick product of 1-amylene by cat head, the tower still is discharged the heavy constituent material;
4) process 3) the thick product of 1-amylene that obtains carries out that rectified purified rectifying tower is a packing tower to remove light constituent, and theoretical plate number is 50, and raw material is by the position charging of the 40th column plate.Working pressure is a normal pressure, and other rectification process condition sees that table 5 is listed.Cat head is discharged the light constituent material, gets tower still material and gets 1-amylene refined prod.
Product yield, the product purity of each embodiment 1-amylene sees that table 6 is listed.
Table 2.
Table 3.
| ? | Tower top temperature (℃) | Tower still temperature (℃) | Reflux ratio |
| Embodiment 1 | 26 | 110 | 6 |
| Embodiment 2 | 29 | 128 | 1 |
| Embodiment 3 | 30 | 125 | 4 |
| Embodiment 4 | 30 | 140 | 3 |
| Embodiment 5 | 30 | 135 | 2 |
| Embodiment 6 | 30 | 138 | 3 |
| Embodiment 7 | 29 | 150 | 2 |
| Embodiment 8 | 27 | 120 | 3 |
| Embodiment 9 | 30 | 132 | 2 |
| Embodiment 10 | 32 | 145 | 1 |
Table 4.
| ? | Tower top temperature (℃) | Tower still temperature (℃) | Reflux ratio |
| Embodiment 1 | 26 | 37 | 50 |
| Embodiment 2 | 28 | 39 | 36 |
| Embodiment 3 | 29 | 40 | 38 |
| Embodiment 4 | 29 | 38 | 30 |
| Embodiment 5 | 30 | 36 | 25 |
| Embodiment 6 | 29 | 35 | 32 |
| Embodiment 7 | 29 | 41 | 34 |
| Embodiment 8 | 27 | 45 | 20 |
| Embodiment 9 | 29 | 38 | 45 |
| Embodiment 10 | 32 | 42 | 40 |
[0038]Table 5.
| ? | Tower top temperature (℃) | Tower still temperature (℃) | Reflux ratio |
| Embodiment 1 | 25 | 36 | 40 |
| Embodiment 2 | 25 | 38 | 38 |
| Embodiment 3 | 26 | 35 | 36 |
| Embodiment 4 | 26 | 37 | 32 |
| Embodiment 5 | 29 | 40 | 25 |
| Embodiment 6 | 27 | 39 | 30 |
| Embodiment 7 | 27 | 42 | 45 |
| Embodiment 8 | 25 | 45 | 20 |
| Embodiment 9 | 28 | 41 | 34 |
| Embodiment 10 | 29 | 40 | 50 |
Table 6.
| ? | 1-amylene product yield (%) | 1-amylene product purity (%) |
| Embodiment 1 | 79.2 | 97.0 |
| Embodiment 2 | 81.0 | 96.8 |
| Embodiment 3 | 80.8 | 97.2 |
| Embodiment 4 | 80.5 | 97.5 |
| Embodiment 5 | 82.2 | 97.3 |
| Embodiment 6 | 81.3 | 97.1 |
| Embodiment 7 | 81.5 | 97.4 |
| Embodiment 8 | 80.9 | 97.0 |
| Embodiment 9 | 79.9 | 97.3 |
| Embodiment 10 | 80.1 | 97.4 |
Claims (5)
1. one kind is separated the method produce the 1-amylene by the Petrocarbon 5 distillate, and this method is a raw material with the surplus Petrocarbon 5 distillate of taking out that extracting has separated behind diolefin and the isopentene, and its process comprises:
1) raw material carries out extracting rectifying, and extraction agent is N, dinethylformamide; Raw material is 1: 5～1: 12 with the feed weight ratio of extraction agent, and the extractant feed temperature is 20～45 ℃, and tower top temperature is 25～36 ℃; Tower still temperature is 60～120 ℃, and working pressure is a normal pressure, and reflux ratio is 1～6; Cat head is discharged carbon five stable hydrocarbon materials, and the tower still gets the material of enrichment 1-amylene and extraction agent;
2) process 1) tower still material carry out rectifying to reclaim extraction agent, tower top temperature is 26～32 ℃, tower still temperature is 110～150 ℃, working pressure is a normal pressure, reflux ratio is 1～6, cat head gets the material of enrichment 1-amylene, the tower still gets extraction agent, the extraction agent recycled;
3) process 2) the cat head material carry out rectifying separation to remove heavy constituent, tower top temperature is 26～32 ℃, tower still temperature is 35～45 ℃, working pressure is a normal pressure, reflux ratio is 20～50, gets the thick product of 1-amylene by cat head, the tower still is discharged the heavy constituent material;
4) process 3) the thick product of 1-amylene that obtains carries out that rectified purified tower top temperature is 25～29 ℃ to remove light constituent, and tower still temperature is 35～45 ℃; Working pressure is a normal pressure; Reflux ratio is 20～50, and cat head is discharged the light constituent material, gets tower still material and gets 1-amylene refined prod.
2. the method for producing the 1-amylene of separating by the Petrocarbon 5 distillate according to claim 1; It is characterized in that process 1) described raw material is 1: 6～1: 10 with the feed weight ratio of extraction agent; The extractant feed temperature is 30～40 ℃, and tower still temperature is 65～100 ℃, and reflux ratio is 1～4.
3. according to claim 1ly separate the method produce the 1-amylene, it is characterized in that process 2 by the Petrocarbon 5 distillate) described tower top temperature is 27～30 ℃, and tower still temperature is 120～140 ℃, and reflux ratio is 1～4.
4. according to claim 1ly separate the method produce the 1-amylene, it is characterized in that process 3 by the Petrocarbon 5 distillate) described tower top temperature is 27～30 ℃, and tower still temperature is 38～42 ℃, and reflux ratio is 30～40.
5. according to claim 1ly separate the method produce the 1-amylene, it is characterized in that process 4 by the Petrocarbon 5 distillate) described tower still temperature is 38～42 ℃, reflux ratio is 30～40.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200710039674A CN101289362B (en) | 2007-04-19 | 2007-04-19 | Process for preparing 1-amylene by separating C5 distillate of petroleum |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200710039674A CN101289362B (en) | 2007-04-19 | 2007-04-19 | Process for preparing 1-amylene by separating C5 distillate of petroleum |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101289362A CN101289362A (en) | 2008-10-22 |
| CN101289362B true CN101289362B (en) | 2012-10-24 |
Family
ID=40033841
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200710039674A Active CN101289362B (en) | 2007-04-19 | 2007-04-19 | Process for preparing 1-amylene by separating C5 distillate of petroleum |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101289362B (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103724194A (en) * | 2012-10-16 | 2014-04-16 | 中国石油化工股份有限公司 | Method for preparing acetic acid sec-pentyl ester |
| CN103333041B (en) * | 2013-07-24 | 2015-09-23 | 上海派尔科化工材料有限公司 | A kind of preparation method of positive amylene |
| CN103333042B (en) * | 2013-07-24 | 2015-09-23 | 上海派尔科化工材料有限公司 | A kind of preparation method of amylene |
| CN104557410B (en) * | 2013-10-11 | 2017-09-29 | 中国石油化工股份有限公司 | A kind of method of the amylene of high-purity 1 |
| CN104557407B (en) * | 2013-10-11 | 2017-10-27 | 中国石油化工股份有限公司 | A kind of 2 pentene isomerization is the method for 1 amylene |
| CN104557409B (en) * | 2013-10-11 | 2018-03-20 | 中国石油化工股份有限公司 | The method of the amylene of high-purity 1 |
| CN105061128B (en) * | 2015-07-31 | 2016-08-10 | 濮阳市新豫石油化工有限责任公司 | A kind of the most poly-C5 of oil extracts dechlorination method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4348260A (en) * | 1979-12-06 | 1982-09-07 | Nippon Zeon Co., Ltd. | Method for inhibiting polymerization of conjugated dienes |
| CN1160035A (en) * | 1996-03-20 | 1997-09-24 | 中国石油化工总公司 | Method for separation of petroleum cracking C5 fraction by liquid phase feeding extraction rectification |
| CN1796341A (en) * | 2004-12-24 | 2006-07-05 | 中国石化上海石油化工股份有限公司 | Refining separation method for coarse piperyene |
-
2007
- 2007-04-19 CN CN200710039674A patent/CN101289362B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4348260A (en) * | 1979-12-06 | 1982-09-07 | Nippon Zeon Co., Ltd. | Method for inhibiting polymerization of conjugated dienes |
| CN1160035A (en) * | 1996-03-20 | 1997-09-24 | 中国石油化工总公司 | Method for separation of petroleum cracking C5 fraction by liquid phase feeding extraction rectification |
| CN1796341A (en) * | 2004-12-24 | 2006-07-05 | 中国石化上海石油化工股份有限公司 | Refining separation method for coarse piperyene |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101289362A (en) | 2008-10-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101289363B (en) | Process for preparing 1-amylene by separating C5 distillate of petroleum | |
| CN101289362B (en) | Process for preparing 1-amylene by separating C5 distillate of petroleum | |
| CN102010285B (en) | Method for extracting methyl cyclopentadiene from ethylene cracked C9 heavy fractions | |
| CN100447118C (en) | Extraction and rectification separation method for normal hexane and methyl cyclopentane | |
| CN101289360B (en) | Process for preparing 2-amylene by separating C5 distillate of petroleum | |
| CN111377800B (en) | Separation device and separation method for coal-to-ethanol liquid phase product | |
| CN103242121B (en) | The working method of normal hexane and benzene extracting rectifying | |
| CN101774879B (en) | Method for simultaneously extracting high-purity beta-methylnaphthalene and indole from coal tar | |
| CN101289361B (en) | Process for preparing 2-amylene by separating C5 distillate of petroleum | |
| CN102633597A (en) | Process of recovering ethanol, propyl alcohol and isobutyl alcohol from polyalcohol-water mixture | |
| CN101412671A (en) | Method for separating isobutyl acetate, ethanol and water by azeotropic distillation | |
| CN109704907B (en) | Method for preparing hexane from raffinate oil | |
| CN106478339A (en) | A kind of isolating cyclopentane and the method for 2,2- dimethylbutane | |
| CN101234947A (en) | Method for removing micro-benzene in solvent oil or hexane refining process | |
| CN105585412A (en) | Method for preparing polymer-grade piperylene | |
| CN101643379A (en) | Preparation method of high-purity 1,3-pentadiene | |
| CN109704908B (en) | Method for preparing hexane from aromatic raffinate oil | |
| CN102399122A (en) | Method for preparing cyclopentadiene and methyl cyclopentadiene | |
| CN104557410B (en) | A kind of method of the amylene of high-purity 1 | |
| CN100503526C (en) | Method for refining crude piperyene | |
| CN104557409B (en) | The method of the amylene of high-purity 1 | |
| CN103570486A (en) | Method for obtaining isoprene from C5 fraction | |
| CN1226261C (en) | Liquid-liquid extraction process of dioxyethyl methane and water solution of ethanol | |
| CN1789223A (en) | Apparatus for extracting coarse 1,3-butadiene by double baffle plated tower and method thereof | |
| CN102675030A (en) | Process method for directly separating petroleum resin raw materials from cracking C9 fraction |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |