EP1379489A1 - Procede de preparation de propylene - Google Patents

Procede de preparation de propylene

Info

Publication number
EP1379489A1
EP1379489A1 EP02745221A EP02745221A EP1379489A1 EP 1379489 A1 EP1379489 A1 EP 1379489A1 EP 02745221 A EP02745221 A EP 02745221A EP 02745221 A EP02745221 A EP 02745221A EP 1379489 A1 EP1379489 A1 EP 1379489A1
Authority
EP
European Patent Office
Prior art keywords
mixture
components
hexene
component
stream
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.)
Withdrawn
Application number
EP02745221A
Other languages
German (de)
English (en)
Inventor
Michael Röper
Jürgen STEPHAN
Götz-Peter SCHINDLER
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
BASF SE
Original Assignee
BASF SE
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Priority claimed from DE2001118634 external-priority patent/DE10118634A1/de
Priority claimed from DE10130958A external-priority patent/DE10130958A1/de
Priority claimed from DE10160726A external-priority patent/DE10160726A1/de
Application filed by BASF SE filed Critical BASF SE
Publication of EP1379489A1 publication Critical patent/EP1379489A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C11/00—Aliphatic unsaturated hydrocarbons
    • C07C11/02—Alkenes
    • C07C11/06—Propene
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C6/00—Preparation of hydrocarbons from hydrocarbons containing a different number of carbon atoms by redistribution reactions
    • C07C6/02—Metathesis reactions at an unsaturated carbon-to-carbon bond
    • C07C6/04—Metathesis reactions at an unsaturated carbon-to-carbon bond at a carbon-to-carbon double bond
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
    • C07C2521/02—Boron or aluminium; Oxides or hydroxides thereof
    • C07C2521/04—Alumina
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • C07C2523/32—Manganese, technetium or rhenium
    • C07C2523/36—Rhenium

Definitions

  • the present invention relates to a process for producing propene from a mixture Ml consisting essentially of
  • Hexenes (components H), optionally olefinic other than ethylene and hexenes
  • the molar proportion of the sum of 2- and 3-hexene in components H is at least 4: 1 to 99: 1, the molar ratio of component E to the sum of components H and Kla is 1: 1 to 100: 1, the ratio of 2-hexene to 3-hexene is at least 2: 1, unless the 3-hexene contained in the mixture is simultaneously subjected to isomerization, which increases the proportion of 2-hexene accordingly.
  • steam crackers operated with naphtha are primarily used to provide unsaturated hydrocarbons which can serve as starting products for the production of further, more highly refined organic compounds.
  • Particularly valuable starting products are ethylene, propylene, butenes and hydrocarbons containing a phenyl ring. Since on the one hand the product range of the steam cracker, as far as the mentioned products of value are concerned, can only be influenced within narrow limits, on the other hand, the demand for the individual products of value in some cases. However, it is very different, there is a particular interest in providing methods to convert some of these valuable products, which are needed to a lesser extent than others due to time or location, to one another in order to be able to respond flexibly to the respective need for the individual valuable products.
  • the US 3785957 relates to the production of gasoline with a high octane number starting from a gasoline containing olefins, ethylene and isobutane.
  • the gasoline containing olefins is disproportionated with ethylene to form a mixture containing propene, butenes and a gasoline fraction consisting of C5 or higher hydrocarbons.
  • This mixture is split into ethylene, propene, butenes, a fraction containing olefinic C5 or C5 to C6 hydrocarbons and a gasoline part containing C6 and higher or C7 and higher hydrocarbons.
  • the fraction containing C5 or C5 to C6 hydrocarbons is split with ethylene in a second disproportionation reaction with a mixture comprising ethylene, propylene and butenes.
  • An alkylation product with a high octane content is produced from the butenes removed therefrom by alkylation with isobutane.
  • the non-prepublished DE-A-10013253 relates to a process for converting olefinic C4 hydrocarbons into propene and hexene.
  • the mixture (Ml) used according to the invention essentially consists of
  • Hexenes (components H) are to be understood as 1-, 2-, or 3-hexene.
  • olefinic hydrocarbons (components Kla) other than ethylene and hexenes
  • pentenes butenes, methylbutenes or methylpentene are particularly suitable.
  • Saturated hydrocarbons such as ethane, propane, butane, isobutane, neopentane, isopentane, methylcyclopropane, are particularly suitable as further inert hydrocarbons (components Klb).
  • the molar ratio of the sum of 2- and 3-hexene on the components H is preferably 10: 1 and particularly preferably 100: 1.
  • the molar ratio of component E to the sum of components H and Kla is preferably 15: 1 and particularly preferably 20: 1.
  • the ratio of 2-hexene to 3-hexene can be chosen freely if the metathesis reaction is carried out under conditions under which isomerization of 3-hexene to 2-hexene takes place at the same time. If this is not the case, the ratio of 2- to 3-hexene is preferably 2.5: 1 and particularly preferably 3: 1.
  • the molar ratio of the sum of components E, H and Kla to components Klb is preferably 4: 1 and particularly preferably 10: 1 and particularly preferably 100: 1.
  • Suitable metathesis catalysts with which the mixture Ml is brought into contact for the desired reaction when the 2- to 3-hexene ratio is at least 2: 1 are catalysts containing a compound of a metal from groups VIb or Vllb of the periodic table Elements.
  • the metathesis catalyst preferably contains an oxide of a metal from group VIb or Vllb of the periodic table.
  • the metathesis catalyst is selected from the group consisting of Re 2 0, W0 3 and Mo0 3 .
  • Such suitable catalysts and their preparation are described, for example, in DE-A-11013253.
  • the reaction can be carried out both in the liquid and in the gas phase.
  • the metathesis is preferably carried out at 0 to 110 ° C and in the gas phase at 150 to 350 °.
  • the pressure is generally 10 to 15 bar if the liquid phase and 1 to 5 bar if the gas phase is used.
  • Catalyst packs are used which, in addition to the aforementioned metathesis catalysts, also contain isomerization catalysts which are different therefrom.
  • the isomerization catalysts contain a metal from groups Ia, Iia, Illb, IVvb, Vb or VIII of the Periodic Table of the Elements or a compound thereof.
  • the isomerization catalyst is preferably selected from the group consisting of RuO, MgO and K 2 CO 3 .
  • the catalysts are generally supported on the usual materials known to the person skilled in the art.
  • suitable materials include Si0 2 , gamma-Al 2 0 3 , MgO or mixtures of these materials.
  • the reaction according to the invention can be carried out batchwise or continuously, e.g. by continuously passing a liquid or gas stream, formed from the mixture Ml, into a reaction zone, bringing it into contact with the metathesis catalyst and continuously removing a stream 2 from the reaction zone.
  • the material flow 2 consists essentially of
  • the components Kla come e.g. Octene, Nonene, or Decene.
  • components E, Pr, B and Pe, a mixture of components H2 and Hx and a mixture of other components are separated from material stream 2 in separate fractions.
  • the mixtures Ml required are generally obtained by using a hydrocarbon fraction (mixture M2) consisting essentially of 2- or 3-hexene, provided the ratio of 2-hexene to 3-hexene is less than 2: 1 mol% Subjects isomerization, whereby 3-hexene is converted to 2-hexene and the defined amounts of component E are added to the reaction mixture. It is also possible to carry out the isomerization on the mixture Ml.
  • catalysts which were listed above in variant 2 of the isomerizing metathesis reaction as those which are added to the metathesis catalysts in order to bring about an isomerization of 3-hexene to 2-hexene (isomerization catalysts).
  • Mixture M2 can be obtained particularly cheaply by using a mixture M3 consisting essentially of
  • Component B obtained from stream 2 is preferably used as component in mixture M3.
  • the components E, H2 and Hx are preferably returned, i.e. used to make mixture Ml.
  • Mixture M3 is preferably provided by
  • Naphtha or another hydrocarbon compound is subjected to a steam cracking or FCC process (fluid catalytic cracking process) and withdraws a C4 hydrocarbon fraction from the stream of material formed in the process
  • a C4 hydrocarbon stream (raffinate I) consisting essentially of isobutene, 1-butene, 2-butene and butanes is produced from the C4 hydrocarbon fraction by selective hydrogenation of the butadienes and butines to butenes or butanes or the butadienes and butines by Extractive distillation removed
  • the mixture M3 can in particular also be provided by first providing a C1-0efin mixture by one of the methods described below and treating it from this mixture analogously to raffinate I.
  • the C 4 -01efin mixtures are generally made from LPG, LNG or MTO streams.
  • LPG means Liquified Petroleum Gas.
  • Liquid gases of this type are defined, for example, in DIN 51 622. They generally contain the hydrocarbons propane, propene, butane, butene and their mixtures, which are used in oil refineries as by-products in the distillation and cracking of petroleum and in natural gas processing in the separation.
  • LNG means Liquified Natural Gas. Natural gas mainly consists of saturated hydrocarbons, which have different compositions depending on their origin and are generally divided into three groups. Natural gas from pure natural gas deposits consists of methane and little ethane.
  • Natural gas from oil deposits also contains larger amounts of higher molecular hydrocarbons such as ethane, propane, isobutane, butane, hexane, heptane and by-products. Natural gas from condensate and distillate deposits contains not only methane and ethane, but also to a considerable extent higher-boiling components with more than 7 carbon atoms. For a more detailed description of liquefied gases and natural gas, reference can be made to the corresponding keywords in Römpp, Chemielexikon, 9th edition.
  • the LPG and LNG used as feedstock particularly include so-called field butanes, as the C4 fraction of the "moist" portions of natural gas and associated petroleum gases are called, which are separated from the gases in liquid form by drying and cooling to about -30 ° C.
  • Field butanes are obtained from this by low-temperature or pressure distillation, the composition of which varies depending on the deposit, but which generally contain about 30% isobutane and about 65% n-butane.
  • the C-01efin mixtures which are derived from LPG or LNG streams, can be obtained in a suitable manner by separating off the C component and dehydrating and feed cleaning.
  • Possible work-up sequences for LPG or LNG streams are dehydrogenation, subsequently separation or partial hydrogenation of the dienes, alkynes and enines and subsequently isolation of the C -01efins.
  • the dehydrogenation can be followed first by the isolation of the C -01efins, followed by the separation or partial hydrogenation of the dienes, alkynes and enines and, if appropriate, further by-products. It is also possible to carry out the sequence isolation of the C -01efine, dehydration, separation or partial hydrogenation.
  • Suitable processes for the dehydrogenation of hydrocarbons are described, for example, in DE-A-100 47 642.
  • the dehydrogenation can, for example, be carried out in a heterogeneously catalyzed manner in one or more reaction zones, with at least some of the heat of dehydrogenation required in at least one reaction zone being combusted directly by hydrogen, hydrogen or hydrocarbons and / or carbon in the presence of an oxygen-containing gas the reaction mixture is generated.
  • the reaction gas mixture which contains the dehydratable hydrocarbon or hydrocarbons is brought into contact with a Lewis acidic dehydrogenation catalyst which has no Bronsted acidity.
  • Suitable catalyst systems are Pt / Sn / Cs / K / La on oxidic supports such as Zr0 2 , Si0 2 , Zr0 2 / Si0 2 , Zr0 2 / Si0 2 / Al 2 0 3 , Al 2 0 3 , Mg (Al) 0.
  • Suitable mixed oxides of the carrier are obtained by successive or joint precipitation of soluble precursors.
  • the LNG stream can, for example, be converted into the C 4 01efin ge via an MTO process.
  • MTO stands for methanol-to-olefin. It is related to the MTG process (Methanol-To-Gasoline). It is a process for the dehydration of methanol over a suitable catalyst, whereby an olefinic hydrocarbon mixture is formed.
  • methanol synthesis can be carried out in advance using the MTO process.
  • C ⁇ feed streams can thus be converted into olefin mixtures from methanol and the MTO process, from which the C 4 -01efins can be separated by suitable methods. The separation can take place, for example, by distillation.
  • a mixture M4 is first prepared by adding ethene from a fraction separated from stream 2, consisting essentially of pentenes (components Pe), so that the mixing ratio of components E: Pe is 5: 1, preferably 10 : 1 is.
  • Mixture M4 mainly contains 1-pentene as component Pe and only 2-pentene as secondary component. However, since 2-pentene is required for the production of propene, the mixture M4 is reacted under the conditions described for the isomerizing metathesis of mixture Ml.
  • either the mixture M5 or component Pe is previously subjected to isomerization in order to achieve a 2-pentene to 1-pentene ratio of at least 2: 1.
  • catalyst packings can be used for the metathesis, which only cause metathesis and no simultaneous isomerization. The same applies here as in the isomerization of 3- to 2-hexene.
  • Creole metathesis of ethylene and 2-pentene can be carried out batchwise or continuously, e.g. by continuously passing a liquid or gas stream formed from the mixture M4 into a reaction zone, bringing it into contact with the metathesis catalyst there and continuously removing a stream 5 from the reaction zone.
  • the material flow 5 consists essentially of
  • components K5a 1 to 50 mol% ethylene 1 to 30 mol% propene 0 to 10 mol% butenes 0 to 10 mol% pentenes - 0 to 5 mol% other olefinic hydrocarbons (components K5b).
  • components E, Pr, B, Pe, K5a and K5b are separated from material stream 5 in separate fractions.
  • Component E is suitable for the preparation of mixture Ml or M5, component Pe of mixture M5.
  • reaction temperature was then increased to 150 ° C. in order to bring about an isomerization of the olefin mixture used.
  • ethylene was then injected to a pressure of 200 bar and this pressure was kept constant over a reaction period of 12 h.
  • reaction temperature was then increased to 150 ° C. in order to bring about an isomerization of the 3-hexene used.
  • ethylene is then injected to a pressure of 200 bar and this pressure is kept constant over a reaction time of 12 h.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

Procédé de préparation de propylène à partir d'un mélange M1 constitué pour l'essentiel d'éthylène (constituant E), d'hexènes (constituant H), éventuellement d'hydrocarbures oléfiniques (constituant K1a) différents de l'éthylène et des hexènes et éventuellement d'autres hydrocarbures inertes (constituant K1b), qui consiste à mettre en contact le mélange M1 avec un catalyseur de métathèse à une température de 20 à 350 °C. Le mélange M1 répond aux conditions suivantes : la proportion molaire de la somme constituée des hexènes 2 et 3 au constituant H est d'au moins 4/1 à 99/1, le rapport molaire du constituant E à la somme des constituants H et K1a est de 1/1 à 100/1, le rapport du 2-hexène au 3-hexène est d'au moins 2/1, dans la mesure où le 3-hexène contenu dans le mélange n'est pas simultanément soumis à une isomérisation par laquelle la part de 2-hexène est augmentée de manière correspondante.
EP02745221A 2001-04-12 2002-04-06 Procede de preparation de propylene Withdrawn EP1379489A1 (fr)

Applications Claiming Priority (7)

Application Number Priority Date Filing Date Title
DE2001118634 DE10118634A1 (de) 2001-04-12 2001-04-12 Verfahren zur Herstellung von Olefinen
DE10118634 2001-04-12
DE10130958 2001-06-27
DE10130958A DE10130958A1 (de) 2001-06-27 2001-06-27 Verfahren zur Herstellung von Propen durch Ethenolyse von Hexen
DE10160726A DE10160726A1 (de) 2001-12-11 2001-12-11 Verfahren zur Herstellung von Propen durch Ethenolyse von Hexen
DE10160726 2001-12-11
PCT/EP2002/003828 WO2002083609A1 (fr) 2001-04-12 2002-04-06 Procede de preparation de propylene

Publications (1)

Publication Number Publication Date
EP1379489A1 true EP1379489A1 (fr) 2004-01-14

Family

ID=27214399

Family Applications (1)

Application Number Title Priority Date Filing Date
EP02745221A Withdrawn EP1379489A1 (fr) 2001-04-12 2002-04-06 Procede de preparation de propylene

Country Status (3)

Country Link
US (1) US20040138512A1 (fr)
EP (1) EP1379489A1 (fr)
WO (1) WO2002083609A1 (fr)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102004009805A1 (de) * 2004-02-28 2005-09-15 Basf Ag Trägerkatalysator definierter Porenverteilung im Bereich der Mesoporen
DE102004041850A1 (de) * 2004-08-27 2006-03-02 Basf Ag Verfahren zur Herstellung von C5-Aldehyden und Propen aus einem 1-Buten- und 2-Buten-haltigen C4-Strom
DE102005009596A1 (de) * 2005-02-28 2006-08-31 Basf Ag Verfahren zur Metathese umfassend die Reinigung der Ausgangsstoffe
EP2196444A1 (fr) * 2008-12-11 2010-06-16 Total Petrochemicals Research Feluy Procédé de fabrication d'alpha-oléfines à partir d'éthanol
KR20140029452A (ko) * 2011-04-20 2014-03-10 코그니스 아이피 매니지먼트 게엠베하 불포화 화합물의 제조 방법
CN102746083B (zh) * 2011-04-22 2014-08-13 中国石油化工股份有限公司 一种低碳烯烃气体的分离工艺
CN102875307B (zh) * 2011-07-11 2016-01-13 中国石油化工股份有限公司 甲醇制丙烯的方法
CN105403477B (zh) * 2015-12-02 2021-02-12 天津众智科技有限公司 一种低温筛选甲醇制烯烃催化剂的方法

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Publication number Priority date Publication date Assignee Title
US3785957A (en) * 1972-01-03 1974-01-15 Phillips Petroleum Co Multistage cleavage of olefins to produce high octane gasoline
US4709115A (en) * 1986-05-15 1987-11-24 The Dow Chemical Company Disproportionation of alkenes
JP2861429B2 (ja) * 1991-02-27 1999-02-24 株式会社デンソー ディーゼル機関の蓄圧式燃料噴射装置
DE4433300C1 (de) * 1994-09-19 1995-11-09 Volkswagen Ag Verfahren und Vorrichtung zur Leerlaufeinstellung einer Brennkraftmaschine
DE59700957D1 (de) * 1996-09-27 2000-02-10 Basf Ag Verfahren zur Herstellung von Propen
DE19805716A1 (de) * 1998-02-12 1999-08-19 Basf Ag Verfahren zur Herstellung von Propen und gegebenenfalls 1-Buten
DE19813720A1 (de) * 1998-03-27 1999-09-30 Basf Ag Verfahren zur Herstellung von Olefinen
AU4925799A (en) * 1998-09-04 2000-03-27 Sasol Technology (Proprietary) Limited Production of propylene
JP3715953B2 (ja) * 2002-07-10 2005-11-16 三菱電機株式会社 燃圧センサの特性補正装置
JP3894179B2 (ja) * 2003-10-02 2007-03-14 トヨタ自動車株式会社 内燃機関の燃料供給装置

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO02083609A1 *

Also Published As

Publication number Publication date
US20040138512A1 (en) 2004-07-15
WO2002083609A1 (fr) 2002-10-24

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