WO2004033400A1 - Verfahren zur trennung von butenen und butanen durch extraktive destillation mit einem polaren extraktionsmittel - Google Patents
Verfahren zur trennung von butenen und butanen durch extraktive destillation mit einem polaren extraktionsmittel Download PDFInfo
- Publication number
- WO2004033400A1 WO2004033400A1 PCT/EP2003/008687 EP0308687W WO2004033400A1 WO 2004033400 A1 WO2004033400 A1 WO 2004033400A1 EP 0308687 W EP0308687 W EP 0308687W WO 2004033400 A1 WO2004033400 A1 WO 2004033400A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- stage
- fraction
- separation
- butenes
- butanes
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
- C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
- C07C7/08—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds by extractive distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/08—Alkenes with four carbon atoms
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C9/00—Aliphatic saturated hydrocarbons
- C07C9/02—Aliphatic saturated hydrocarbons with one to four carbon atoms
- C07C9/10—Aliphatic saturated hydrocarbons with one to four carbon atoms with four carbon atoms
Definitions
- the invention relates to a process for the separation of butenes and butanes from a stream containing C 4 hydrocarbons by extractive distillation with a polar extractant.
- Butenes and butanes are industrially sought-after products that are mostly obtained by processing C 4 hydrocarbon cuts from steam or naphtha crackers.
- the various isomers of butenes and butanes and butadiene are present in varying proportions in the raw material sources available.
- Butadiene can either be converted to n-butenes by hydrogenation or removed from these mixtures by extractive distillation.
- EP 501 848 describes the separation of a C 4 section freed from butadiene by extractive distillation with an extracting agent such as N-methylpyrrolidone (NMP) or DMF in three stages: In the first stage, the C 4 - hydrocarbon mixture with the extracting agent is used an extractive distillation column. Here, the olefinic constituents dissolve in the extractant, so that the less soluble aliphatic constituents can be separated off. For further separation or for the recovery of the extracting agent, a partial desorption of the butenes from the extract is then carried out under a pressure of 4 to 5 bar. For the remaining recovery of the extractant, the extract is then boiled out at normal pressure and a temperature of 140 to 170 ° C.
- NMP N-methylpyrrolidone
- JP 692 876 discloses the use of dimethylformamide as a polar extractant for butene / butane separation. Furthermore, this publication describes that after the extractive distillation and the separation of the aliphatic constituents from the feed Hydrocarbon mixture, most of the polar extractant is recovered by a desorption step at 1 to 2 atmospheres with recycling of most of the extractant. The butene-containing fraction is freed from the butenes in a cleaning stage at elevated pressure of 1 to 15 atmospheres; the pure extractant thus obtained is in turn returned to the extraction distillation stage. According to the examples, the extractant still contains large proportions of butenes, which are recycled with the extractant, ie are circulated. This is energetically and economically unfavorable.
- the present invention relates to a process for the separation of butenes and butanes by extractive distillation using a polar extractant
- stage b) a reflux ratio of stage b) to stage a) of 0.01-0.5 kg / kg, preferably 0.05-0.2 kg / kg, has proven successful.
- the reflux ratio is defined here as the ratio of the amount returned to the amount of product.
- the reflux ratio corresponds to the quotient of the material flows 9 and 8.
- Stage b) is usually operated at 1.0 to 5 bar. If stage a) has a higher pressure stage, the part of the low boiler fraction recycled from stage b) in stage a) can be precompressed to the pressure of stage a).
- FIG. 1 Such a procedure is outlined by FIG. 1: Here the butane / butene mixture (1) is separated in the extraction stage (2) into the butanes (3) and a fraction (4) containing the butenes and a polar extractant.
- Material stream (4) is separated in the distillation stage (5) into a high-boiling fraction (6), which contains the polar extracting agent and possibly also butenes, and a low-boiling fraction (7), which comprises the butenes and any residues of extracting agent , Material flow (7) is completely or partially separated off and, if necessary, further processed (8) and / or returned to the extraction stage (2) after an optional compressor stage (10).
- the compressor stage 10 can also be arranged directly behind the distillation stage, so that the low boilers obtained therefrom are fully condensed and then divided into product and recycle stream in liquid form.
- the recycle stream can be cooled.
- This cooling stage should bring the current down to -10 to +55 ° C, preferably 0-35 ° C.
- the process according to the invention has a further separation stage c).
- the low boiler fraction from stage b) is wholly or partly separated in a second separation stage c) into a butene-containing fraction and a fraction containing the polar extracting agent, and the fraction containing the polar extracting agent is returned to the distillative separation of stage b).
- the separation by distillation in stage b) is preferably carried out at a pressure of 1 to 5, in particular 1 to 3, bar.
- the temperatures vary according to this pressure at 120 - 190 ° C, especially 125 - 160 ° C. In this way, a large part of the polar extractant is already carefully separated from the olefinic components at relatively low temperatures.
- the second separation in step c) of the process according to the invention is preferably carried out by distillation at a pressure of 1-10 bar, in particular 3-7 bar. This process variant is explained in more detail by FIG. 2 as follows.
- the feed hydrocarbon mixture (1) is reacted in the extraction stage (2) with a polar extractant, so that the butanes (3) can be separated off as a low boiler fraction.
- the butenes and the polar extractant are fed as a bottom fraction (4) to a distillation separation (5), a mixture of butenes and the polar extractant being separated off as the low boiler fraction (6).
- the low boiler fraction usually still contains 1-6% by weight of extractant. If water is present, the solvent fraction of the low boiler fraction mainly consists of water, in the case of the NMP / water system this fraction consists of approx. 1.5 - 3% water with approx. 100 - 1000 ppm NMP.
- Material stream (6) is then worked up in a further separation stage (7) onto the pure butenes (8), small polar amounts of the extracting agent and possibly water being recycled as high boiler fraction (9) into the first separation stage (5).
- the stream (9) may also contain butenes in addition to the polar extractant.
- the high boiler fraction (10) obtained in the first separation stage (5), which comprises most of the polar extractant, is returned to the extraction stage (2).
- a compressor and / or cold stage (11) is also expedient in this variant of the method.
- the temperatures range from 40 to 100 ° C according to the set pressure.
- the second separation stage c) is not carried out by separation by distillation, but rather by cooling the low boiler fraction from stage b) to -10 to +55 ° C., preferably 0-55 ° C., in particular 0-35 ° C.
- the pressures required here range from 1.0 to 5, preferably 1-3.0, bar. This variant can be used advantageously wherever inexpensive cooling energy is available. Furthermore, the investments required for the pressure-resistant apparatus in the other process variant are eliminated.
- the second separation stage (7) is not designed as a distillation separation, but as a top condenser of the column (5).
- the returns (9) or the separation of the butenes (8) are carried out analogously.
- the compressor and / or cold stage (11) is omitted in this variant.
- dimethylformamide (DMF), N-methylpyrrolidone, acetonitrile, furfural, N-formylmorpholine or dimethylacetamine can be used as the polar extracting agent.
- the extractants used can either be anhydrous or virtually anhydrous or else in a mixture of 0.1 to 20 wt.%, Preferably 3 to 18 wt.%, Particularly preferably 5 to 12 wt.%, In particular 8 to 9 wt. -%, are used with water.
- the extraction distillation of stage a) is preferably carried out at a pressure of 2 to 15 bar and a temperature of 40 to 100 ° C.
- Such columns are usually operated in countercurrent, ie the extractant is introduced into the column from above and the stream to be extracted from below.
- the C 4 stream can also be fed in the middle part of the column.
- the C 4 hydrocarbon stream to be extracted is preferably evaporated upstream of the column and brought into contact with the polar extractant as a gas stream in a mass ratio of 15: 1-6: 1, preferably 12: 1-6: 1 (gas: liquid) ,
- the column is expediently equipped with internals or packing elements in order to build up the largest possible exchange surface.
- the butane-containing mixture (n- and isobutane) is then drawn off in gaseous form at the top of the column and used for further use.
- the bottom of the column can be heated externally or internally, all or part of the bottom fraction being fed to a distillation separation in stage b). Packings, bell or valve trays have proven particularly useful as internals for the extractive distillation column.
- the C 4 stream obtained at the top of the column (stream 3 in the figures) is completely condensed and partially recycled to backwash the polar extractant. Return ratios of 0.5 to 2, in particular 1: 1, have proven themselves here.
- the bottom fraction obtained from stage a) is then depressurized and preferably passed to the top of the distillation column in stage b).
- This column is preferably filled with packing and is operated in countercurrent at a bottom temperature of 120 to 160 ° C.
- the column bottom is returned to the extraction distillation according to stage a).
- the low boiler fraction to be drawn off at the top which contains the butenes and the small amounts of the polar extracting agent mentioned, is cooled to a temperature of 30 to 60 ° C. and then fed to the cleaning stage c).
- the low boiler fraction of stage b) first passes through a compressor stage and is compressed to the pressure stages mentioned.
- the purification stage (7) can also be operated as a countercurrent distillation system in which the low boiler fraction from stage b) is introduced into the bottom of the column.
- the polar extractant enriched in the sump is not returned to the extraction distillation of stage a) but exclusively to the cleaning stage b).
- a reflux ratio of 0.001-0.1 kg / kg, preferably 0.01-0.1 kg / kg has proven successful.
- the reflux ratio is defined here as the quotient of the amount returned in stage b) to the amount introduced in cleaning stage c). In Fig. 2 this corresponds to the ratio of the currents 9: 6.
- part of the top product is preferably returned to the column to improve the separation performance.
- a further, small separation stage which follows the separation stage c), is recommended, with which the butenes are drawn off as the bottom product and an aqueous phase is separated off by means of a decanter at the top of the column and is returned to the separation stage b) if necessary, is premixed with the polar extractant.
- the separation stage c) is carried out without a compressor as a top condenser of stage b). For this it is necessary to fully condense the low boiler fraction of stage b) to a temperature of approx. 10-25 ° C. Part of the liquid fraction is returned to column b) in countercurrent.
- An NMP / H2O mixture with about 8% by weight of water was used as solvent.
- the extractive distillation column (2) had a diameter of 80 mm and was equipped with 70 bubble-cap trays.
- the outgassing column (5) also had a diameter of 80 mm and was equipped with 30 bubble trays.
- the butane product stream (3) was completely condensed and partially returned to the column (2) at a reflux ratio of 1 kg / kg.
- the butene product stream (7) obtained was cooled to 50 ° C. and drawn off completely in gaseous form, ie there was no butene recycling (9) to the extractive distillation column (2).
- the liquid stream obtained on cooling to 50 ° C. was fed back into the column (5).
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Analytical Chemistry (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2004542290A JP2006502204A (ja) | 2002-09-16 | 2003-08-06 | 極性抽出剤を用いる抽出蒸留によりブテンとブタンを分離する方法 |
AU2003253384A AU2003253384A1 (en) | 2002-09-16 | 2003-08-06 | Method for separating butenes and butanes by extractive distillation provided with a polar extraction agent |
US10/527,322 US20060096849A1 (en) | 2002-09-16 | 2003-08-06 | Method for separating butenes and butanes by extractive distillation provided with a polar extraction agent |
EP03807776A EP1539660A1 (de) | 2002-09-16 | 2003-08-06 | Verfahren zur trennung von butenen und butanen durch extraktive destillation mit einem polaren extraktionsmittel |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10242923A DE10242923A1 (de) | 2002-09-16 | 2002-09-16 | Verfahren zur Trennung von Butenen und Butanen durch extraktive Destillation mit einem polaren Extraktionsmittel |
DE10242923.5 | 2002-09-16 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2004033400A1 true WO2004033400A1 (de) | 2004-04-22 |
Family
ID=31724795
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2003/008687 WO2004033400A1 (de) | 2002-09-16 | 2003-08-06 | Verfahren zur trennung von butenen und butanen durch extraktive destillation mit einem polaren extraktionsmittel |
Country Status (8)
Country | Link |
---|---|
US (1) | US20060096849A1 (de) |
EP (1) | EP1539660A1 (de) |
JP (1) | JP2006502204A (de) |
KR (1) | KR20050057375A (de) |
CN (1) | CN1310857C (de) |
AU (1) | AU2003253384A1 (de) |
DE (1) | DE10242923A1 (de) |
WO (1) | WO2004033400A1 (de) |
Families Citing this family (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102005023549A1 (de) * | 2005-05-21 | 2006-11-23 | Oxeno Olefinchemie Gmbh | Verfahren zur Oligomerisierung von Butenen |
CN101050159B (zh) * | 2007-05-17 | 2010-06-23 | 新疆独山子天利高新技术股份有限公司 | 分离丁烷与丁烯的方法及其专用装置 |
DE102008007081B4 (de) | 2008-01-31 | 2018-12-06 | Evonik Degussa Gmbh | Verfahren zur Herstellung von n-Buten-Oligomeren und 1-Buten aus technischen Mischungen I von C4-Kohlenwasserstoffen |
CN102690158A (zh) * | 2012-06-06 | 2012-09-26 | 中国石油集团东北炼化工程有限公司锦州设计院 | 一种从炼厂碳四组分中分离出高纯度正丁烷的工业化方法 |
CN102718618A (zh) * | 2012-06-06 | 2012-10-10 | 中国石油集团东北炼化工程有限公司锦州设计院 | 一种从炼厂碳四组分中分离出高纯度异丁烷的方法 |
HUE044163T2 (hu) | 2012-11-07 | 2019-10-28 | Lummus Technology Inc | Szelektív olefin extrakció |
CN103193577B (zh) * | 2013-03-25 | 2014-12-10 | 烟台大学 | 一种用三元混合溶剂萃取精馏分离丁烷与丁烯的方法 |
CN104557391A (zh) * | 2013-10-10 | 2015-04-29 | 湖南中创化工股份有限公司 | 一种带溶剂回收系统的用溶解和/或分散有银盐的乙腈溶剂分离丁烷与丁烯的方法 |
CN105712828B (zh) * | 2014-12-04 | 2017-12-22 | 中国石油化工股份有限公司 | 一种甲乙酮生产用c4原料的提纯方法 |
CN105712820B (zh) * | 2014-12-04 | 2018-10-12 | 中国石油化工股份有限公司 | 一种醚后碳四的提浓新工艺 |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0216991A1 (de) * | 1985-09-11 | 1987-04-08 | Krupp Koppers GmbH | Verfahren zur Trennung von paraffinischen und olefinischen C4-Kohlenwasserstoffen |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3496069A (en) * | 1967-11-09 | 1970-02-17 | Petro Tex Chem Corp | Purification of unsaturated hydrocarbons by extractive distillation with recycle of stripper overhead |
DE1916255C3 (de) * | 1969-03-29 | 1979-04-05 | Krupp-Koppers Gmbh, 4300 Essen | Verfahren zur Trennung von Kohlenwasserstoffgemischen, die Paraffine, Monoolefine, Diolefine sowie gegebenenfalls geringe Mengen stärker ungesättigte Kohlenwasserstoffe enthalten |
DE1908126C3 (de) * | 1969-02-19 | 1974-06-27 | Heinrich Koppers Gmbh, 4300 Essen | Verfahren zur Trennung von gesättigten Kohlenwasserstoffen und Olefinen |
DE2724365C3 (de) * | 1977-05-28 | 1979-09-06 | Basf Ag, 6700 Ludwigshafen | Verfahren zum Trennen eines C4 -Kohlenwasserstoffgemisches durch extraktive Destillation |
FR2674245B1 (fr) * | 1991-03-20 | 1994-05-27 | Inst Francais Du Petrole | Procede de separation de butenes et de butanes par distillation extractive. |
JP2842091B2 (ja) * | 1992-09-11 | 1998-12-24 | 日本ゼオン株式会社 | 高純度1−ブテン及び2−ブテンの取得方法 |
-
2002
- 2002-09-16 DE DE10242923A patent/DE10242923A1/de not_active Withdrawn
-
2003
- 2003-08-06 KR KR1020057004517A patent/KR20050057375A/ko not_active Application Discontinuation
- 2003-08-06 AU AU2003253384A patent/AU2003253384A1/en not_active Abandoned
- 2003-08-06 JP JP2004542290A patent/JP2006502204A/ja active Pending
- 2003-08-06 WO PCT/EP2003/008687 patent/WO2004033400A1/de active Application Filing
- 2003-08-06 US US10/527,322 patent/US20060096849A1/en not_active Abandoned
- 2003-08-06 CN CNB038219271A patent/CN1310857C/zh not_active Expired - Fee Related
- 2003-08-06 EP EP03807776A patent/EP1539660A1/de not_active Withdrawn
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0216991A1 (de) * | 1985-09-11 | 1987-04-08 | Krupp Koppers GmbH | Verfahren zur Trennung von paraffinischen und olefinischen C4-Kohlenwasserstoffen |
Also Published As
Publication number | Publication date |
---|---|
KR20050057375A (ko) | 2005-06-16 |
DE10242923A1 (de) | 2004-03-18 |
JP2006502204A (ja) | 2006-01-19 |
CN1310857C (zh) | 2007-04-18 |
EP1539660A1 (de) | 2005-06-15 |
AU2003253384A1 (en) | 2004-05-04 |
CN1681754A (zh) | 2005-10-12 |
US20060096849A1 (en) | 2006-05-11 |
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