CN101205165A - Preparation of isopentane solvent for polyolefins by separation technique - Google Patents
Preparation of isopentane solvent for polyolefins by separation technique Download PDFInfo
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- CN101205165A CN101205165A CNA2006101653157A CN200610165315A CN101205165A CN 101205165 A CN101205165 A CN 101205165A CN A2006101653157 A CNA2006101653157 A CN A2006101653157A CN 200610165315 A CN200610165315 A CN 200610165315A CN 101205165 A CN101205165 A CN 101205165A
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Abstract
The invention relates to a method for adopting the separation process to prepare an isopentane solvent for polyolefin. With the light hydrocarbon of the petrochemical plant or alkane obtained by separating the C5 fraction which is the cracking by-product generated from an ethylene plant as the raw materials, the raw materials are subject to the distillation separation in a light ends removal column, a de-heavy fractionator and a final product tower so as to obtain the isopentane solvent for polyolefin; wherein, the number of theoretical plates of the light ends removal column ranges from 20 to 100, the operating pressure ranges from 0.6 to 1.5MPa, the top temperature ranges from 20 to 60 DEG C and the bottom temperature ranges from 70 to 190 DEG C; the number of theoretical plates of de-heavy fractionator ranges from 30 to 110, the operating pressure ranges from 0.1 to 1.0MPa, the top temperature ranges from 20 to 80 DEG C and the bottom temperature ranges from 80 to 190 DEG C ; the number of theoretical plates of the product tower ranges from 40 to 140, the operating pressure 0.1 to 0.6MPa, the top temperature ranges from 20 to 60 DEG C and the bottom temperature ranges from 30 to 150 DEG C; the content of the produced isopentane olefin is lower than 30ppm and the index of the produced isopentane olefin meets the requirements on production of the polyolefin device.
Description
Technical field
The present invention relates to a kind of separation method of iso-pentane, specifically, relating to a kind of is raw material with refinery's lighter hydrocarbons or the C5 fraction of ethylene plant's cracking by product through the alkane after separating, and adopts the precise distillation technology, separates the method for isoolefine content less than the pentane solvent of 30ppm of producing from lighter hydrocarbons.
Background technology
Iso-pentane is mainly used in the solvent of whipping agent, refrigeration agent and production full density polythene, linear low density polyethylene at present.The iso-pentane that is used for whipping agent, refrigeration agent, the olefin(e) centent index request is relatively low, adopts conventional distillation technology can obtain qualified product, and the purpose product has iso-pentane, Skellysolve A, pentamethylene or the mixture between them.
Along with improving constantly of polyethylene production technology, also more and more higher to the index request of solvent iso-pentane, polyethylene device is increased to 30ppm to olefin(e) centent index request in the iso-pentane by 500ppm.
CN1232816 discloses and has a kind ofly prepared the method for iso-pentane by three fractionation and hydrogenation technique, but the purity of the iso-pentane of its preparation does not reach the requirement of polyethylene device.
US6286335, US6173584, CN1300930 disclose the separation method and the device of paraffins mixture, but its separate object, do not contain C5 alkene in the paraffins mixture, can't be applied to the purification of the iso-pentane that polyethylene device uses, " reduce the research and the application of iso-pentane acid number " equally, also be unsuitable for the purification of the iso-pentane that polyethylene device uses, the document adopts rectification method purification iso-pentane, removes CO2 from iso-pentane.
The producer of domestic production iso-pentane has increased hydrogenation and has taken off the alkene unit for olefin(e) centent index request in the iso-pentane is increased to 30ppm by 500ppm, to take off the alkene in the iso-pentane, causes complex process, and production cost raises.
Summary of the invention
The objective of the invention is to, the preparation method of a kind of polyolefine with the iso-pentane solvent is provided, through the alkane after separating, obtain to satisfy the iso-pentane product of polyethylene device requirement by the cracking by product C5 fraction of separating ethene factory.
For achieving the above object, technical scheme of the present invention is as follows:
A kind of separating technology that adopts is produced the method for polyolefine with the iso-pentane solvent, is raw material with refinery's lighter hydrocarbons or the C5 fraction of ethylene plant's cracking by product through the alkane after separating, raw material is through the rectifying separation of lightness-removing column, weight-removing column and last product tower, obtain polyolefine iso-pentane solvent, wherein: the number of theoretical plate of lightness-removing column is 20-100, working pressure is 0.6-1.5MPa, tower top temperature 20-60 ℃, and column bottom temperature 70-190 ℃; The number of theoretical plate of weight-removing column is 30-110, and working pressure is 0.1-1.0MPa, tower top temperature 20-80 ℃, and column bottom temperature 80-190 ℃; The number of theoretical plate of product tower is 40-140, and working pressure is 0.1-0.6MPa, tower top temperature 20-60 ℃, and column bottom temperature 30-150 ℃.
Described product tower is a precise rectification tower.
The rectifying separation order of described raw material is according to the sequencing of lightness-removing column, weight-removing column and product tower.Perhaps according to the sequencing of weight-removing column, lightness-removing column and product tower.
Described raw material is that the C5 fraction of ethylene plant's cracking by product is through the alkane after separating.In the raw material, isopentane content is higher, and carbon pentaene hydrocarbon content is very low, helps the economy of technology.Refinery's lighter hydrocarbons preferably.1-amylene content compares less than 0.000425 with isopentane content in the raw material.
Produce the process of iso-pentane for adopting hydrogenation-rectification process, because along with the catalyzer prolongation of duration of service, the reduction of catalyst activity, cause the hydrogenation intermediates to use the rectifying separation technology not reach the olefin(e) centent index request, and rectification process need be become precise distillation technology, also within the scope of the present invention.
Described lightness-removing column is the rectifying tower that removes the component lighter than iso-pentane, and weight-removing column is the rectifying tower that removes the component heavier than iso-pentane.
The present invention proposes and utilize the precise distillation technology, adopt three tower process of different separation sequences to produce the iso-pentane method, comprise two kinds of schemes.
Scheme one (process flow sheet such as Fig. 1): the step that comprises is
(1) raw material that contains than low-carbon (LC) pentaene hydrocarbon enters lightness-removing column, and the component lighter than iso-pentane distillates from cat head, and iso-pentane and heavier component distillate at the bottom of tower.
(2) iso-pentane and heavier component enter thick product tower, and the component heavier than iso-pentane distillates at the bottom of tower, and thick product iso-pentane distillates from cat head.In this tower, part 1-amylene, 2-methyl-1-butene alkene, Skellysolve A and heavier component distillate at the bottom of tower, and cat head is the extremely low thick iso-pentane product of 1-amylene, 2-methyl-1-butene alkene of higher iso-pentane of purity and content.
(3) thick product enters the product tower, and cat head obtains qualified iso-pentane product, and components such as iso-pentane, amylene distillate at the bottom of tower.Cat head obtains olefin(e) centent and is lower than 30ppm iso-pentane product, and the bottomsstream is the very low Skellysolve A of iso-pentane, amylene and content.
The step that scheme two comprises is
(1) raw material that contains than low-carbon (LC) pentaene hydrocarbon enters weight-removing column, and iso-pentane and lighter component distillate from cat head, than heavy the distillating at the bottom of tower of iso-pentane.
(2) iso-pentane and lighter component enter lightness-removing column, and the component lighter than iso-pentane distillates from cat head, and the carbon pentaene hydrocarbon of iso-pentane and trace distillates at the bottom of tower.
(3) iso-pentane and trace amounts of olefin enter the product tower, and part iso-pentane and carbon pentaene hydrocarbon distillate at the bottom of tower, and cat head obtains the qualified product iso-pentane.
The present invention adopts the precise distillation technology to produce iso-pentane, and the alkene in the product iso-pentane contains and heavily is lower than 30ppm, and its index reaches the requirement that polyolefin device is produced.
Description of drawings
Fig. 1: polyolefine iso-pentane solvent preparation technology general flow chart
Embodiment
Utilize precise distillation technology, adopt and take off gently, take off heavy three-column process flow earlier, the raw material composition sees Table one.
At first, raw material enters lightness-removing column, the operational condition of lightness-removing column is: cat head working pressure 0.8MPa, tower bottom pressure 1.0MPa, stage number 90,18 blocks of plates of feed entrance point, reflux ratio is 6.8, the component lighter than iso-pentane distillates from cat head, and iso-pentane and distillate at the bottom of the tower than the heavy component of iso-pentane and to enter thick product tower, cat head, tower base stream are formed and seen Table two, three.
The operational condition of thick product tower is: cat head working pressure 0.2MPa, tower bottom pressure 0.4MPa, stage number 75,41 blocks of plates of feed entrance point, reflux ratio is 9.9, and iso-pentane and a small amount of amylene distillate from cat head, enter the product tower, the component heavier than iso-pentane distillates at the bottom of tower, and cat head, tower base stream composition see Table four, five.
Product tower operational condition is: cat head working pressure 0.2MPa, tower bottom pressure 0.4MPa, stage number 80, feed entrance point piece plate 35, reflux ratio is 8.8, product iso-pentane and minute quantity amylene distillate from cat head, and iso-pentane, amylene and a spot of Skellysolve A distillate at the bottom of tower, and cat head, tower base stream composition see Table six, seven.
Table one raw material is formed (wt%)
(wt%) formed in the logistics of table two lightness-removing column top
(wt%) formed in the logistics of table three lightness-removing column top
The thick product overhead stream of table four is formed (wt%)
The thick product tower base stream of table five is formed (wt%)
Table six product overhead stream is formed (wt%)
Table seven product tower base stream is formed (wt%)
Claims (5)
1. one kind is adopted separating technology to produce the method for polyolefine with the iso-pentane solvent, it is characterized in that: is raw material with refinery's lighter hydrocarbons or the C5 fraction of ethylene plant's cracking by product through the alkane after separating, rectifying separation through lightness-removing column, weight-removing column and last product tower, obtain polyolefine iso-pentane solvent, wherein: the number of theoretical plate of lightness-removing column is 20-100, working pressure is 0.6-1.5MPa, tower top temperature 20-60 ℃, and column bottom temperature 70-190 ℃; The number of theoretical plate of weight-removing column is 30-110, and working pressure is 0.1-1.0MPa, tower top temperature 20-80 ℃, and column bottom temperature 80-190 ℃; The number of theoretical plate of product tower is 40-140, and working pressure is 0.1-0.6MPa, tower top temperature 20-60 ℃, and column bottom temperature 30-150 ℃.
2. method according to claim 1 is characterized in that: described product tower is a precise rectification tower.
3. method according to claim 1 is characterized in that: the rectifying separation order of described raw material is according to the sequencing of lightness-removing column, weight-removing column and product tower.
4. method according to claim 1 is characterized in that: the rectifying separation order of described raw material is according to the sequencing of weight-removing column, lightness-removing column and product tower.
5. method according to claim 1 is characterized in that: 1-amylene content compares less than 0.000425 with isopentane content in the described raw material.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006101653157A CN100572345C (en) | 2006-12-18 | 2006-12-18 | A kind of separating technology that adopts is produced the method for polyolefine with the iso-pentane solvent |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006101653157A CN100572345C (en) | 2006-12-18 | 2006-12-18 | A kind of separating technology that adopts is produced the method for polyolefine with the iso-pentane solvent |
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| CN101205165A true CN101205165A (en) | 2008-06-25 |
| CN100572345C CN100572345C (en) | 2009-12-23 |
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| CNB2006101653157A Active CN100572345C (en) | 2006-12-18 | 2006-12-18 | A kind of separating technology that adopts is produced the method for polyolefine with the iso-pentane solvent |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103073376A (en) * | 2013-02-22 | 2013-05-01 | 南京炼油厂有限责任公司 | Separation process of mixed pentane |
| CN109305877A (en) * | 2017-07-26 | 2019-02-05 | 抚顺伊科思新材料有限公司 | Thick light dydrocarbon produces high alkene light dydrocarbon, pentane, isopentane and pentamethylene method |
| CN115651704A (en) * | 2022-11-29 | 2023-01-31 | 中国石油化工股份有限公司洛阳分公司 | Method for producing pentane foaming agent by using reformed oil |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1055282C (en) * | 1995-09-21 | 2000-08-09 | 上海石油化工高等专科学校 | Catalytic hydrogenation process of industrial C5 fraction to produce pentane |
| EP0940381B1 (en) * | 1998-03-05 | 2003-11-05 | BP Köln GmbH | Process for the recovery of cyclopentane and/or cyclopentene |
| US6173584B1 (en) * | 1999-09-03 | 2001-01-16 | Air Products And Chemicals, Inc. | Multieffect distillation |
| US6286335B1 (en) * | 1999-09-03 | 2001-09-11 | Air Products And Chemicals, Inc. | Processes for multicomponent separation |
| CN100441554C (en) * | 2005-01-28 | 2008-12-10 | 中国石油化工股份有限公司 | Method of utilizing cracked, C5 fraction |
-
2006
- 2006-12-18 CN CNB2006101653157A patent/CN100572345C/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103073376A (en) * | 2013-02-22 | 2013-05-01 | 南京炼油厂有限责任公司 | Separation process of mixed pentane |
| CN109305877A (en) * | 2017-07-26 | 2019-02-05 | 抚顺伊科思新材料有限公司 | Thick light dydrocarbon produces high alkene light dydrocarbon, pentane, isopentane and pentamethylene method |
| CN115651704A (en) * | 2022-11-29 | 2023-01-31 | 中国石油化工股份有限公司洛阳分公司 | Method for producing pentane foaming agent by using reformed oil |
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| CN100572345C (en) | 2009-12-23 |
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