EP2029638A1 - Fabrication de polyisobutène réactif et sensiblement exempt d'halogène à partir de mélanges d'hydrocarbures en c4 pauvres en isobutène - Google Patents

Fabrication de polyisobutène réactif et sensiblement exempt d'halogène à partir de mélanges d'hydrocarbures en c4 pauvres en isobutène

Info

Publication number
EP2029638A1
EP2029638A1 EP07729909A EP07729909A EP2029638A1 EP 2029638 A1 EP2029638 A1 EP 2029638A1 EP 07729909 A EP07729909 A EP 07729909A EP 07729909 A EP07729909 A EP 07729909A EP 2029638 A1 EP2029638 A1 EP 2029638A1
Authority
EP
European Patent Office
Prior art keywords
mixture
isobutene
range
weight
butene
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Withdrawn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
EP07729909A
Other languages
German (de)
English (en)
Inventor
Richard J. Blackborow
Hans Peter Rath
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
Application filed by BASF SE filed Critical BASF SE
Priority to EP07729909A priority Critical patent/EP2029638A1/fr
Publication of EP2029638A1 publication Critical patent/EP2029638A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F10/04—Monomers containing three or four carbon atoms
    • C08F10/08—Butenes
    • C08F10/10—Isobutene
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F2/00—Processes of polymerisation
    • C08F2/01—Processes of polymerisation characterised by special features of the polymerisation apparatus used
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F110/00—Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F110/04—Monomers containing three or four carbon atoms
    • C08F110/08—Butenes
    • C08F110/10—Isobutene

Definitions

  • the present invention relates to a process for preparing reactive and substantially halogen-free, especially fluorine-free polyisobutenes from low-isobutene C 4 - hydrocarbon mixtures.
  • Such reactive polyisobutenes are used as intermediates for the preparation of additives for lubricants and fuels, as described, for example, in DE-A-2702604.
  • the preparation of these additives includes, for example, the formation of polyisobutene-maleic anhydride adducts or the alkylation of, for example, phenols.
  • the preparation of reactive polyisobutenes usually takes place by means of cationic polymerization of isobutene or isobutene-containing streams in the presence of suitable Lewis acids as catalyst.
  • suitable catalysts are boron trifluoride and boron trifluoride complexes.
  • C4 feedstocks which in addition to isobutene further C4 hydrocarbons, such as 1- and 2-butene, butane and isobutane , contain.
  • the isobutene concentrations of conventional feedstocks are often in the range of 8 to 40 wt .-% isobutene or even less than 5 wt .-% isobutene and thus well below the optimum concentration range.
  • a relatively high content of 1-butene is problematic in that, in the case of cationic polymerization of the isobutene-containing feedstock, the polymer chain is preferably terminated by copolymerized 1-butene at complete isobutene conversions.
  • a 1-butene terminated polyisobutene molecule has a strong tendency to bind fluorine, eg from the boron trifluoride catalyst, so that the fluorine content of polyisobutenes from C4 feedstocks with a relatively high proportion of 1-butene is significantly higher compared to polyisobutenes from C4 feedstocks with a lower proportion of 1-butene.
  • a high fluorine content of the polyisobutenes makes them unattractive for many applications, for example in the fuel sector, due to the corrosive properties of HF or the formation of dioxins.
  • EP-A-0523838 describes a process for the isomerization of linear olefins to isoolefins, e.g. from n-butenes to isobutene, in the presence of zeolites as isomerization catalysts.
  • US Pat. No. 5,043,523 describes the isomerization of olefins, such as C4-olefins, in the presence of low-sodium siloxane-modified ⁇ -aluminum oxide as isomerization catalyst.
  • DE 3118199 describes a process for the isomerization of the C4 component in C3-C4 hydrocarbon mixtures using fluorinated aluminum oxide in the presence of water or steam.
  • EP 0192059 describes the dehydroisomerization of butane to isobutene using a zirconia-supported chromium oxide / niobium pentoxide catalyst.
  • EP-A-0671419 describes a process for the preparation of polyisobutene, in which a C4-hydrocarbon mixture is first subjected to a pretreatment to reduce the content of 1-butene and then polymerized, the pretreated hydrocarbon mixture.
  • US 4,435,609 describes a process for the hydroisomerization of 1-butene to 2-butenes using a metal of VIII. Subgroup as a catalyst in the presence of hydrogen.
  • EP-A-0288362 describes a process in which butadiene present in a C 4 hydrocarbon mixture is hydrogenated and at the same time 1-butene is isomerized to 2-butene.
  • the reaction takes place in the presence of two different catalysts, wherein the C4 feedstock first a hydrogenation catalyst (Pd in combination with Au and / or Pt, supported on alumina or silica) for the hydrogenation of butadiene and then an isomerization (on alumina or silica supported Pd) happened.
  • a hydrogenation catalyst Pd in combination with Au and / or Pt, supported on alumina or silica
  • FR-A-2515171 describes the selective oligomerization of isobutene in a C 4 hydrocarbon mixture.
  • EP-A-0628575 and WO 99/64482 describe the preparation of reactive polyisobutenes by cationic polymerization of isobutene or isobutene-containing hydrocarbon streams in the presence of BF 3 in combination with alcohols or primary or secondary dialkyl ethers.
  • WO 97/06189 describes the preparation of halogen-free, reactive polyisobutenes by polymerization of isobutene or isobutene-containing hydrocarbon streams in the presence of a catalyst which comprises, in addition to an oxygen-containing zirconium compound, at least one oxygen-containing compound of at least one element from I, II, III, IV ., V., VII. Or VIII. Subgroup or from II., IM., IV., V. or VI. Main group contains and does not contain technically effective amounts of halogen.
  • the inventive method should allow the production of polyisobutenes with the narrowest possible molecular weight distribution.
  • the object was achieved by a process for preparing reactive and substantially halogen-free polyisobutenes, comprising the following steps:
  • step (ii) optionally hydroisomerizing at least a portion of the mixture Ia obtained in step (i) to obtain a mixture Ib which contains at least 5% by weight less 1 -butene than the mixture Ia;
  • step (iii) optionally recovering substantially pure isobutene from at least part of the mixture Ia obtained in step (i) or from at least part of the mixture Ib obtained in step (ii);
  • step (iv.5) the isobutene obtained in step (iii) with a mixture II of C 4 hydrocarbons other than mixtures Ia and Ib, or
  • step (iv.6) the mixture Ib obtained in step (ii) with a mixture II of C4 hydrocarbons other than mixtures Ia and Ib;
  • step (v) reaction of the mixture Ia obtained in step (i) or the mixture Ib obtained in step (ii) or the mixture obtained in step (iv) or the isobutene obtained in step (iii) in a cationic polymerization in the presence of a BF 3 containing catalyst.
  • reactive polyisobutenes are understood as meaning polyisobutenes which are at least 60 mol%, preferably at least 70 mol%, more preferably at least 80 mol% and in particular at least 90 mol%, e.g. about 95 mole percent, terminal double bonds based on the total number of polyisobutene macromolecules.
  • they are vinylidene groups.
  • essentially halogen-free or fluorine-free means that the polyisobutene contains at most 50 ppm, preferably at most 20 ppm, more preferably at most 15 ppm and especially at most 10 ppm, for example at most 5 ppm or at most 2 ppm or at most 1 ppm halogen, specifically fluorine, based on the total weight of the polyisobutene.
  • the ppm data here refer to ppm by weight, ie 1 ppm corresponds to 10 " 4 wt .-%.
  • a mixture I of C 4 -hydrocarbons which has at most 10% by weight, based on the total weight of mixture I, of isobutene.
  • the mixture I at most 8 wt .-% and particularly preferably at most 5 wt .-%, based on the total weight of the mixture I, of isobutene.
  • Suitable mixtures I of C 4 hydrocarbons result, for example, after one or more processing steps, in the hydrocarbon scale separation carried out on an industrial scale in the course of petroleum processing, for example by cracking such as fluid catalytic cracking (FCC), thermal cracking, hydroprocessing. Cracking or dehydration of isobutane.
  • FCC fluid catalytic cracking
  • hydroprocessing hydroprocessing
  • C4 cuts are hydrocarbon mixtures whose main constituent are hydrocarbons having 4 carbon atoms, such as butane, isobutane, 1- and 2-butene and isobutene.
  • C4 cuts can be obtained, for example, by fluid catalytic cracking or steam cracking of gas oil or by steam cracking of liquefied gas or naphtha or by dehydrogenation of isobutane or butane.
  • the composition differs depending on whether the raffinate was recovered in a steam cracker or FC cracker, which methods of isobutene removal were used, and which feeds were used in the cracker.
  • raffinate II from steam crackers with naphtha as a feedstock and the removal of isobutene by etherification usually has substantially the following composition:
  • Isobutene in the range of 1 to 10 wt .-%, preferably in the range of 1, 5 to 3 wt .-%, 1-butene: in the range of 40 to 60 wt .-%, preferably in the range of 45 to 55 wt %, cis-2-butene: in the range of 5 to 15% by weight, preferably in the range of 5 to 10% by weight, trans-2-butene: in the range of 10 to 20% by weight, preferably in the range from 12 to 18% by weight, n-butane: in the range from 10 to 20% by weight, preferably in the range from 12 to 20% by weight, Isobutane: in the range of 5 to 10% by weight, or preferably in the range of 6 to 10% by weight.
  • Raffinate II from FCC units is more dependent on the source of the crude oil and, after removal of isobutene by etherification, usually has essentially the following composition:
  • Isobutene in the range of 0.5 to 3 wt .-%, preferably in the range of 1 to 2 wt .-%, 1-butene: in the range of 15 to 25 wt .-%, preferably in the range of 17 to 24 wt %, cis-2-butene: in the range of 10 to 25% by weight, preferably in the range of 12 to 33% by weight, trans-2-butene: in the range of 15 to 25% by weight, preferably in the range from 17 to 23% by weight, n-butane: in the range from 10 to 20% by weight, preferably in the range from 10 to 17% by weight, isobutane: in the range from 20 to 35% by weight. %. preferably in the range of 22 to 33% by weight.
  • the term "substantially” means that the content of further components in the specified compositions is at most 5% by weight, preferably at most 1% by weight, based on the total weight of the raffinate compositions those skilled in the art, that when using technical hydrocarbon mixtures in particular also fractions of hydrocarbons having less or more than 4 carbon atoms can be contained as further components .
  • a raffinate IIP usually has essentially the following composition:
  • Isobutene in the range from 1 to 5% by weight, preferably in the range from 1 to 5% by weight,
  • 1-butene in the range of 1 to 5 wt.%, Preferably in the range of 2 to 4 wt.%, Cis-2-butene: in the range of 10 to 25 wt.%, Preferably in the range of 15 to 22% by weight, Trans-2-butene: in the range of 40 to 50 wt .-%, preferably in the range of 42 to 48 wt .-%, n-butane: in the range of 25 to 40 wt .-%, preferably in the range of 28 to 38% by weight,
  • Isobutane in the range of 10 to 20% by weight, preferably in the range of 12 to 18% by weight.
  • a raffinate IM usually has substantially the following composition:
  • Isobutene in the range of 0 to 3% by weight, preferably in the range of 0.1 to 1% by weight,
  • 1-butene in the range of 0 to 3 wt .-%, preferably in the range of 0.1 to 1 wt .-%
  • cis-2-butene in the range of 1 to 5 wt .-%, preferably in the range of 1, 5 to 3 wt .-%
  • trans-2-butene in the range of 5 to 30 wt .-%, preferably in the range of 8 to 20 wt .-%
  • n-butane in the range of 40 to 70 wt .-%, preferably in the range of 45 to 65 wt .-%
  • Isobutane in the range of 10 to 30 wt .-%. preferably in the range of 15 to 25 wt .-%.
  • suitable mixtures I of C 4 -hydrocarbon are also obtained from C 4 sections which have been depleted in isobutene, for example by polymerization to polyisobutene.
  • An example of this is the proportion of this C4 mixture remaining after the production of polyisobutene from raffinate I.
  • the mixture I used is preferably a raffinate II from a steam cracker or from an FCC unit or a raffinate II P or a raffinate III from a steam cracker.
  • the cited raffinates in each case have in each case one of the abovementioned compositions.
  • the mixture I used has a content of not more than 0.5% by weight and preferably not more than 0.2% by weight, based on the total weight of the mixture I, of butadiene.
  • step (i) of the process according to the invention an isomerization of at least part of the C4 hydrocarbons contained in the mixture I takes place.
  • the isomerization is carried out under such conditions that the resulting mixture Ia contains at least 5% by weight more isobutene than the mixture I used (ie when mixture I ⁇ wt .-% isobutene, based on the total weight of the mixture I, contains, the mixture Ia obtained in step (i) contains at least (x + 5) wt .-% isobutene, based on the total weight of the mixture Ia).
  • the mixture Ia contains at least 10 wt .-%, more preferably at least 15 wt .-% and in particular at least 20 wt .-% more isobutene than the mixture used I.
  • the content of isobutene of the mixture Ia obtained in step (i) is preferably at least 10% by weight, more preferably at least 15% by weight and in particular at least 20% by weight, based on the total weight of the mixture Ia.
  • the isomerization reaction in step (i) is preferably a dehydroisomerization or a skeletal isomerization.
  • both isomerization forms can proceed side by side.
  • dehydrations may also take place, e.g. from isobutane to isobutene.
  • skeletal isomerization is understood as meaning a rearrangement reaction in which a methyl group formally migrates.
  • An example of this is the rearrangement of 2-butene to isobutene.
  • dehydroisomerization is understood as meaning the dehydrogenation of an alkane to the corresponding alkene, combined with skeletal isomerization, the latter taking place before, simultaneously with or after the dehydrogenation.
  • An example of this is the dehydroisomerization of n-butane to isobutene.
  • transformations in order to increase the space / time yields, are generally carried out at comparatively high temperatures, typically in the range of 300 to 650 ° C.
  • the isomerization in step (i) is at a temperature in the range of 350 to 600 ° C.
  • the dehydroisomerization takes place to avoid excessive dehydration, preferably in the presence of hydrogen.
  • the skeletal isomerization preferably takes place in the presence of hydrogen and / or water vapor.
  • the isomerization can be carried out both under reduced pressure, at ambient pressure and under overpressure.
  • pressure here refers to the total pressure which is composed of the pressure of the hydrocarbon mixture I and the pressure of the optionally present hydrogen and / or water vapor.
  • the isomerization is carried out under excess pressure, preferably at a pressure of 1, 5 to 20 bar, in particular 2 to 10 bar.
  • the isomerization preferably takes place in the gas phase or above the critical temperature.
  • step (i) is generally carried out in the presence of suitable catalysts.
  • Suitable catalysts for the skeleton isomerization are, for example, aluminum oxides, in particular ⁇ -aluminum oxides, which are preferably distinguished by a low content of alkali metals and alkaline earth metals and which are optionally siloxane-modified, and zeolites. Zeolites are ordered porous crystalline aluminosilicates having a defined structure and cavities connected via channels. Suitable catalysts are described, for example, in EP 523838, US Pat. No. 5,043,523, US Pat. No. 4,436,949 and DE 31 18199 A1, to which reference is hereby fully made.
  • Suitable catalysts for the dehydroisomerization are, for example, aluminum oxides, in particular ⁇ -aluminum oxides, aluminosilicates in porous form (eg bauxite, clay, kaolin), which are optionally supported and activated with phosphoric, boric or fluoric acid, and metal oxides of secondary group metals , eg
  • Chromium oxide, niobium oxide and the like preferably being supported, e.g. on zirconia.
  • Suitable catalysts are described, for example, in EP 192059, US Pat. No. 4,704,497, US Pat. No. 4,806,624 and EP 51291 1, to which reference is hereby made in their entirety.
  • step (i) Whether one selects the isomerization conditions in step (i) in accordance with the conditions described above for a skeletal isomerization or rather for a hydroisomerization depends mainly on the hydrocarbon mixture I used in step (i). If this is relatively high in alkanes, it will be more likely to choose conditions favoring a dehydroisomerization reaction, while for mixtures I with a low level of alkanes, it would be desirable to select conditions that favor skeletal isomerization. On the other hand, the conditions which favor dehydroisomerizations or skeletal isomerizations do not differ so much from one another, that as a rule both types of isomerization proceed side by side.
  • the mixture Ia obtained in step (i) can be subjected to hydroisomerization.
  • Hydroisomerization in the context of the present invention means the rearrangement of olefinic double bonds in which a hydrogen atom formally migrates. An example of this is the double bond rearrangement in the isomerization of 1-butene to 2-butene.
  • step (ii) gives a mixture II whose content of 1-butene is at least 20% by weight, preferably at least 40% by weight, more preferably at least 60% by weight and in particular at least 80% % By weight, based on the 1 -butene contained in the mixture Ia.
  • the mixture Ib obtained in step (ii) contains at most 10% by weight, more preferably at most 7% by weight, more preferably at most 5% by weight and especially at most 3% by weight, e.g. at most 2% by weight or at most 1% by weight of 1-butene, based on the total weight of the mixture Ib.
  • the hydroisomerization is carried out at comparatively low temperatures, preferably at 0 to 200 ° C, more preferably at 20 to 100 ° C.
  • the hydroisomerization of step (ii) is usually carried out in the presence of hydrogen.
  • the reaction mixture which is composed of the partial pressure of the hydrocarbon mixture Ia used in step (ii) and the partial pressure of the hydrogen which is generally present.
  • hydroisomerization conditions are suitably chosen so that essentially only optionally present dienes (especially butadiene) and alkynes (especially acetylene and butynes) are hydrogenated and on the other hand isomerize 1-butene to 2-butene.
  • Suitable catalysts are, for example, transition metal catalysts, such as palladium or platinum.
  • the metal catalysts are supported, e.g. on alumina, silica or zirconia.
  • Suitable catalysts are described, for example, in GB-A-2057006, which is hereby incorporated by reference.
  • Some of the suitable catalysts, e.g. Palladium on alumina are commercially available (e.g., from Sudchemie).
  • the reaction is preferably carried out such that the mixture produced in step (i) is converted into a cooler reaction zone with a catalyst suitable for hydroisomerization, this reaction zone being arranged in the same reactor as the reaction zone for the isomerization reaction of step (i) can as well as in another reactor.
  • step (ii) is carried out above all when polyisobutenes with a low halogen content, especially fluorine content, are to be obtained and the content of 1-butene in the mixture Ia from step (i) is relatively large, for example at least 5% by weight. % or even at least 10 wt .-% is.
  • the content of 1-butene in the mixture Ia is especially great when a hydrocarbon stream is used as the mixture I, which has a relatively high content of 1-butene, for example at least 5 wt .-% or at least 10 wt .-%, as is the case, for example, with raffinate II and / or when the content of 1-butene in mixture Ia increases as a result of the isomerization reaction of step (i) compared with mixture I, for example to at least 5% by weight or at least 10% by weight, for example because the isomerization conditions, especially higher temperatures, also favor the formation of 1-butene.
  • step (ii) is preferably carried out when in step (i) a mixture I containing at least 5% by weight of 1-butene, e.g. a mixture other than raffinate IIP or raffinate III, such as raffinate II, and / or when, in step (i), a mixture Ia containing at least 5% by weight of 1-butene is obtained.
  • a mixture I containing at least 5% by weight of 1-butene e.g. a mixture other than raffinate IIP or raffinate III, such as raffinate II
  • step (ii) can be dispensed with despite a relatively high proportion of 1-butene in the mixture Ia obtained in step (i), if the optional step (iii) is carried out in which substantially pure isobutene is obtained, which is incorporated in the Polymerization reaction of step (v) is used or which is mixed in step (iv) with a isobutene-poorer mixture, eg with the mixture Ia obtained in step (i), which not only increases the isobutene content in this isobutene-poorer mixture, but at the same time decreases the proportion of 1-butene, and this mixture is then subjected to polymerization.
  • substantially pure isobutene which is optionally obtained in step (iii), is meant in the context of the present invention an isobutene-containing mixture which is at least 75% by weight, preferably at least 85% by weight, especially preferred. at least 95 wt .-% isobutene, based on the total weight of the isobutene-containing mixture contains.
  • the isobutene-containing mixture may also be pure isobutene, i. by at least 99% isobutene, act.
  • step (iii) substantially pure isobutene is recovered by a distillation of the mixture Ia or of the mixture Ib.
  • Suitable distillation devices and distillation conditions are known in the art and described for example in FR 2528033, which is incorporated herein by reference.
  • this separation variant is especially suitable for mixtures Ia and Ib which do not contain a high proportion of 1-butene, eg at most 10% by weight or at most 5% by weight of 1-butene.
  • this separation variant also with mixtures which are richer in 1-butene, if the mixture of the isobutene obtained from this separation variant is subsequently obtained in step (iv) in such a way that mixtures II are obtained with sufficiently low 1-butene contents, for example by mixing this relative to 1-butene Isobutene with a 1 Ib-enriched mixture Ib.
  • step (iii) the recovery of substantially pure isobutene comprises the following steps:
  • the selective oligomerization of isobutene in raffinate streams is basically known and described, for example, in FR 2515171, to which reference is hereby fully made.
  • the removal of volatile constituents from the isobutene oligomers takes place by means of distillation in the conventional manner known to the person skilled in the art.
  • Essentially pure isobutene can be obtained from the isobutene oligomers by cleavage.
  • the depolymerization of isobutene oligomers is basically known and described, for example, in H. Schurbock, Polyisobutylene and isobutylene copolymers, Springer Verlag, 1959, pages 23-26, to which reference is hereby fully made.
  • temperatures in the range from 200 to 450 ° C. and the presence of modified aluminum trioxide or silicon dioxide are suitable.
  • step (iii) the recovery of substantially pure isobutene comprises the following steps:
  • suitable alcohols are methanol, ethanol, n-propanol, isopropanol, n-butanol, sec-butanol, isobutanol (2-methylpropan-1-ol), n-pentanol, 2- and 3-pentanol, neopentanol, n-hexanol and Positional isomers thereof.
  • Preferred alcohols are primary alcohols such as methanol, ethanol, n-propanol, n-butanol, isobutanol, n-pentanol and n-hexanol. Most preferably, methanol or isobutanol is used, with isobutanol (2-methylpropan-1-ol) being even more preferred.
  • the selective etherification of isobutene present in the mixture Ia or Ib is carried out by conventional etherification processes, as described, for example, in Ullmann's Encyclopedia of Industrial Chemistry, 5th Edition on CD-ROM, Wiley-VCH, Chapter “Methyl tert-Butyl Ether", Chapter 4 " Production “and chapter” Butenes ", Chapter ⁇ ” Upgrading of butenene "are described, to which reference is hereby made in their entirety.
  • the removal of volatile constituents from the resulting tert-butyl ethers is carried out by distillation in the usual manner known to those skilled in the art.
  • the tert-butyl ethers can be split back into isobutene monomers and the alcohol used.
  • the optional mixing step (iv) serves to optimize isobutene-containing mixtures with regard to their composition, in particular their isobutene and 1-butene content, for the polymerization. This avoids having to subject an entire suboptimal C4 hydrocarbon stream to the process steps (i) and, if necessary, (ii) and / or (iii) prior to the polymerization.
  • step (i) the mixture Ia obtained in step (i) is only partially subjected to step (ii) and then the mixture Ib obtained is mixed with the proportion of Ia not reacted in step (ii).
  • the mixture Ia obtained in step (i) or the mixture Ib obtained in step (ii) or both may be substantially pure with the product obtained in step (iii) Isobutene be mixed, for example, if the amount of isobutene contained in the mixtures Ia and / or Ib is not sufficiently high and / or if the 1-butene content present in one of the components (especially in the mixture Ia or in isobutene) is too high.
  • the essentially pure isobutene obtained in step (iii) or the mixture Ib obtained in step (ii) can be mixed with C 4 hydrocarbon streams other than mixture Ia or Ib (mixture II).
  • Suitable mixtures II are, for example, the mixture I used in step (i), raffinate I or C 4 cuts of FCC units.
  • Preferred mixtures II are Raffinate I and C 4 cuts from FCC units.
  • composition of raffinate I depends on whether liquefied petroleum gas, naphtha or mixtures thereof were used as the feedstock, with naphtha resulting in a raffinate I with higher isobutene contents.
  • the raffinate I obtained from steam crackers has essentially the following composition:
  • Isobutene in the range of 35 to 55% by weight, preferably in the range of 35 to 48% by weight
  • 1-butene in the range of 25 to 35% by weight, preferably in the range of 27 to 33% by weight.
  • trans-2-butene in the range of 5 to 15% by weight, preferably in Range from 6 to 13% by weight
  • n-butane in the range from 5 to 15% by weight, preferably in the range from 7 to 13% by weight
  • isobutane in the range from 2 to 10% by weight, preferably in the range of 3 to 8% by weight
  • the C 4 cut obtained from FCC units has essentially the following composition:
  • Isobutene in the range of 10 to 20% by weight, preferably in the range of 12 to 18% by weight
  • 1-butene in the range of 10 to 20% by weight, preferably in the range of 12 to 20% by weight.
  • % cis-2-butene: in the range of 10 to 20% by weight, preferably in the range of 12 to 18 wt%
  • trans-2-butene in the range of 10 to 25 wt%, preferably in the range of 12 to 22 wt%
  • n-butane in the range of 5 to 15 wt .-%, preferably in the range of 7 to 13 wt .-%
  • isobutane in the range of 15 to 25 wt .-%, preferably in the range of 7 to 23 wt .-%.
  • Hydrocarbons according to step (iv) of the process according to the invention increase the availability of isobutene, which can be fed to a polymerization for the preparation of reactive polyisobutenes.
  • those embodiments of the method according to the invention are made possible, which allow an economical utilization of C4 streams for the production of reactive polyisobutenes, without the isobutene having to be isolated from the entire amount of the C4 streams used.
  • the isobutene is obtained in substantially pure form from a portion of the C 4 hydrocarbons used as mixture I after isomerization. This is done as described above by the separation of the isobutene from the mixture Ia or Ib (step (Ni)).
  • the isobutene monomers thus obtained in substantially pure form can be used for the enrichment of available C 4 - hydrocarbon mixtures. In this way, optimum isobutene concentrations in the reaction mixtures intended for polymerization can be adjusted in a simple manner.
  • the pure isobutene separated off as described above can be blended directly with isobutene-rich C 4 -hydrocarbon mixtures such as raffinate I or FCC-C 4 cuts.
  • C 4 -Raffinatströme the comparatively low levels of isobutene of z.
  • the individual mixture components used in step (iv) may be of the same or different origin.
  • essentially pure isobutene (from step (Ni)) is mixed in step (iv) with a mixture Ia (from step (i)) and / or a mixture Ib (from step (N)).
  • the mixture Ia, the mixture Ib and the substantially pure isobutene from the same or from different mixtures I of C 4 hydrocarbons originate.
  • substantially pure isobutene in step (iv) is mixed with a relatively isobutene-rich C4 cut, for example with raffinate I.
  • step (iv) it has proved to be particularly advantageous to adjust the mixing ratio in step (iv) such that the resulting mixture has a content of isobutene of preferably at least 30% by weight, more preferably at least 40% by weight, in particular at least 50% by weight and especially at least 60% by weight, based in each case on the total weight of the mixture obtained in step (iv).
  • the catalyst used is boron trifluoride, often in combination with a suitable donor (cocatalyst, complexing agent).
  • suitable cocatalysts are alcohols, carboxylic acids, aldehydes, ketones, nitriles, phenols and dialkyl ethers.
  • the resulting Lewis acceptor-donor complex has (also) Bronsted acid properties when using protic donors, such as alcohols or carboxylic acids.
  • Particularly suitable complexes have both Lewis and Brönsted acid properties.
  • the polymerization is generally carried out at a temperature of -100 ° C to
  • the components obtained in step (iii), from which the substantially pure isobutene is separated off, and / or the components obtained in step (v) after the polymerization, from which the formed polyisobutene is separated, are recycled back to step (i).
  • These components obtained in step (iii) are largely C4 hydrocarbons other than isobutene.
  • the components obtained in step (v) are, for the most part, unpolymerized C 4 -hydrocarbons (isobutene and C 4 -hydrocarbons different therefrom) and / or isobutene oligomers.
  • the recycling is particularly preferably carried out when these components obtained in step (iii) or (v) have a low content of 1-butene, for example at most 5% by weight or at most 2% by weight, based on the total weight of the components so they do not need to be used in step (ii).
  • the method of the invention comprises step (i) and step (v), i. steps (i) and (v) are mandatory while steps (ii), (iii) and (iv) are optional.
  • the method according to the invention comprises step (i), step (ii), optionally step (iii), optionally step (iv) and step (v), i. steps (i), (ii) and (v) are mandatory while steps (iii) and (iv) are optional.
  • the process according to the invention comprises step (i), optionally step (ii), step (iii), optionally step (iv) and step (v), i. steps (i), (iii) and (v) are mandatory while steps (ii) and (iv) are optional.
  • the method according to the invention comprises step (i), optionally step (ii), step (iii), step (iv) and step (v), i. Steps (i), (iii), (iv) and (v) are mandatory while step (ii) is optional.
  • the method according to the invention comprises step (i), step (ii), step (iii), optionally step (iv) and step (v), i. steps (i), (ii), (iii) and (v) are mandatory while step (iv) is optional.
  • the method according to the invention comprises step (i), step (ii), step (iii), step (iv) and step (v), ie all 5 steps (i), (ii), (iii ), (iv) and (v) are mandatory.
  • the polyisobutenes prepared by the process according to the invention have a number average molecular weight M n of preferably from 100 to 10,000, more preferably from 500 to 5000 and in particular from 800 to 3000, for example about 1000 or about 1500 or about 2000 or about 2500.
  • M n and M w relate to values determined by gel permeation chromatography (GPC) using polyisobutene standards.
  • the polyisobutenes prepared by the process of the present invention have at least 60 mole%, more preferably at least 70 mole%, more preferably at least 80 mole%, and most preferably at least 90 mole%, e.g. about 95 mole percent terminal double bonds based on the total number of polyisobutene macromolecules.
  • the terminal double bonds are vinylidene groups ( ⁇ -double bond) or 2-methyl-2-engroups ( ⁇ -double bonds).
  • the terminal double bonds are vinylidene groups ( ⁇ -double bond); i.e.
  • the polyisobutenes prepared by the process of the present invention preferably have at least 60 mole%, more preferably at least 70 mole%, more preferably at least 80 mole%, and most preferably at least 90 mole%, e.g. about 95 mol%, terminally arranged vinylidene double bonds, based on the total number of polyisobutene macromolecules.
  • the proportion of terminal double bonds is determined by means of 1 H-NMR spectroscopy.
  • the polyisobutenes prepared by the process according to the invention are distinguished by the fact that they are substantially halogen-free, especially essentially fluorine-free.
  • Halogens such as fluorine may be present in particular in the form of fluoroorganic compounds.
  • the content of fluorine in the reactive polyisobutenes is at most 0.005 wt .-%.
  • the halogen and especially the fluorine content in the polyisobutenes prepared according to the invention is preferably at most 0.005% by weight, more preferably at most 0.002% by weight, more preferably at most 0.0015% by weight, even more preferably at most 0.001% by weight. , for example, at most 5x10 " 4 wt .-% or at most 2x10 " 4 wt .-%, and in particular at most 1x10 "4 wt .-%, based on the total weight of the polyisobutenes.
  • the fluorine content is determined by conventional methods, e.g. determined by combustion analysis with subsequent wet analysis.
  • M n and M w values were carried out by means of GPC (polyisobutene standards).
  • the content of terminal vinylidene groups was determined by means of 1 H-NMR.
  • the fluorine content was determined by wet and combustion analysis.
  • the catalyst used here was a zirconium-based catalyst which was prepared in accordance with EP-A-192059, Example 1 b), the niobium content being 0.1 mol per mol of ZrO 2 and no chromium oxide being used. After calcining at 650 ° C. for two hours, the catalyst was obtained as a powder with 40 ⁇ 60 mesh and an oxygen surface area of 40 m 2 / g.
  • the dehydroisomerization zone was at an absolute Hydrogen pressure of 5 bar operated at 560 ° C. The load was 5 kg of reaction mixture per hour and kg of catalyst. After one hour, gas samples were taken and analyzed.
  • This reactor effluent was fed to a second lower temperature isomerization zone. 342 strand diameter 2 mm, strand length 2-6 mm, surface; in the second isomerization zone an alumina catalyst (was 95% alumina, 5% SiO 2, Siral ® 5, Degussa, into a paste with formic acid, pelletized and 2 h at 350 ° C calcined m 2 / g) are used.
  • the second isomerization zone was operated at 70 ° C at a flow rate of 1 kg reaction mixture per hour and per kg of catalyst.
  • the discharge of C4 hydrocarbons from the second isomerization zone had a content of isobutene of 39 wt .-% and a content of 1-butene of 5 wt .-%, each based on the total weight of the discharge on.
  • the polymerization was carried out analogously to EP-A-628575, Example 1.
  • a loop reactor equipped with an integrated circulating pump (tube diameter 10 mm, volume 100 ml)
  • 600 g of the discharge from the second isomerization zone was conducted for one hour to carry out the polymerization reaction.
  • a catalyst was generated in situ from a BF3-2-butanol complex (22 mmol BF3, 37 mmol 2-butanol).
  • the reactor was cooled so that the internal temperature was -13 ° C.
  • the isobutene conversion was 60%, the average residence time 6.6 minutes.
  • the reaction effluent in a stirred vessel was continuously admixed with 100 ml / h of 10% strength aqueous NaOH and the remaining liquid gas was evaporated at 40.degree.
  • the polymer had a fluorine content of 9 ppm.
  • alumina catalyst (95% alumina, 5% SiO 2, Siral ® 5, Degussa, slurried in water, treated with 0.2% aqueous Na2CO3 solution, filtered off, dried overnight at 100 ° C, strand granulated and calcined at 350 ° C., strand diameter 2 mm, strand length 2-6 mm, surface area 327 m 2 / g).
  • the skeletal isomerization zone was operated at an absolute hydrogen pressure of 5 bar and a temperature of 425 ° C.
  • the load was 2 kg of reaction mixture per hour and per kg of catalyst.
  • the output from the skeleton isomerization zone had a content of isobutene of 22 wt .-% and a content of 1-butene of 12 wt .-%, each based on the total weight of the discharge on.
  • the effluent from the skeletal isomerization zone was fed to a reactor for conducting an etherification reaction.
  • the reaction mixture was reacted with sec-butyl alcohol.
  • the mixture thus obtained was subjected to fractional distillation. In this way, a fraction of pure sec-butyl tert-butyl ether could be obtained. This fraction was split back into sec-butyl alcohol and isobutene in a separate cracking reaction.
  • the isobutene obtained in this case had a purity of 99% by weight.
  • the isobutene obtained in this way was used for the preparation of reactive polyisobutene.
  • a circulation reactor consisting of a 7.1 m long Teflon hose with an inner diameter of 6 mm, was passed over the 100 l / h reactor contents with a gear pump in a circle. Tube and pump had a capacity of 200 ml. Teflon tube and pump head were in a cooling bath cooled to -23.8 ° C via a cryostat.
  • a mixture of 300 g / h of isobutene and 300 g / h of hexane was dried over a molecular sieve 3A to ⁇ 3 ppm water, pre-cooled to 23.8 ° C and fed through a capillary with 2 mm inner diameter to the reactor.
  • BF3 and isopropanol / diisopropyl ether as a complexing agent were fed into the Hexanzulauf.
  • the BF3 feed was adjusted to 23.5 mmol and the total amount of feed of the mixture of hexane, isopropanol and diisopropyl ether was adjusted so that an isobutene conversion of 92% was achieved.
  • Example 3 A stream of raffinate Il P of the following composition:
  • Example 2 a zirconium-based catalyst according to Example 1 was used.
  • the dehydroisomerization zone was operated at 565 ° C and 5 bar absolute hydrogen pressure.
  • the load was 5 kg of reaction mixture per hour and per kg of catalyst.
  • the effluent from the dehydroisomerization zone contained 18% by weight of isobutene and 12% by weight of 1-butene.
  • This discharge was brought into contact with an acidic fixed-bed catalyst according to Example 1 of EP 843688 at 10 ° C. The resulting discharge was subjected to fractional distillation.
  • a bottoms fraction was obtained containing oligomers of isobutene and in particular dimers, trimers and tetramers of isobutene. This bottoms fraction was converted to substantially pure isobutene by cracking at 280 ° C over an aluminum / AIF3 based catalyst (fluorine content 7.8%).
  • the isobutene thus obtained was used analogously to Example 2 for the preparation of reactive polyisobutene.
  • the polymer had a content of terminal vinylidene groups of 95 mol%.
  • the fluorine content in the obtained polymer was less than 1 ppm.
  • the reaction mixture used for Examples 4 to 7 for the polymerization of isobutene monomers was obtained in each case by mixing or enriching different C4 streams with essentially pure isobutene.
  • the mixed isobutene was obtained as described in Example 3.
  • the raffinate used for blending in Example 4 is a raffinate I from the C4 fraction of a predominantly naphtha-operated steam cracker having the following composition: 1-Butene 29.0% by weight cis-2-butene 4.5% by weight trans-2-butene 7.7% by weight isobutene 45.4% by weight n-butane 9.3% by weight -%
  • Example 5 a C4 stream from the catalytic cracker of a refinery of the following composition was used for the mixing:
  • Example 7 a raffinate was IM of the following composition:
  • the blend was made such that the reaction mixture intended for polymerization had an isobutene content of 60% by weight, based on the total weight of the reaction mixture.
  • the polymerization of isobutene was carried out analogously to Example 2. This was adjusted to a flow rate of 600 g / h reaction mixture, 70 mmol BF3 / h, 40 mmol / h isopropanol and 80 mmol / h diisopropyl ether.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

La présente invention concerne un procédé de fabrication de polyisobutène réactif et sensiblement exempt d'halogène, notamment exempt de fluor, à partir de mélanges d'hydrocarbures en C<SUB>4</SUB> pauvres en isobutène.
EP07729909A 2006-06-06 2007-06-05 Fabrication de polyisobutène réactif et sensiblement exempt d'halogène à partir de mélanges d'hydrocarbures en c4 pauvres en isobutène Withdrawn EP2029638A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP07729909A EP2029638A1 (fr) 2006-06-06 2007-06-05 Fabrication de polyisobutène réactif et sensiblement exempt d'halogène à partir de mélanges d'hydrocarbures en c4 pauvres en isobutène

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP06114991 2006-06-06
EP07729909A EP2029638A1 (fr) 2006-06-06 2007-06-05 Fabrication de polyisobutène réactif et sensiblement exempt d'halogène à partir de mélanges d'hydrocarbures en c4 pauvres en isobutène
PCT/EP2007/055534 WO2007141277A1 (fr) 2006-06-06 2007-06-05 Fabrication de polyisobutène réactif et sensiblement exempt d'halogène à partir de mélanges d'hydrocarbures en c4 pauvres en isobutène

Publications (1)

Publication Number Publication Date
EP2029638A1 true EP2029638A1 (fr) 2009-03-04

Family

ID=38509068

Family Applications (1)

Application Number Title Priority Date Filing Date
EP07729909A Withdrawn EP2029638A1 (fr) 2006-06-06 2007-06-05 Fabrication de polyisobutène réactif et sensiblement exempt d'halogène à partir de mélanges d'hydrocarbures en c4 pauvres en isobutène

Country Status (5)

Country Link
US (1) US20100234542A1 (fr)
EP (1) EP2029638A1 (fr)
KR (1) KR20090014372A (fr)
CN (1) CN101460530A (fr)
WO (1) WO2007141277A1 (fr)

Families Citing this family (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR101458404B1 (ko) * 2013-01-17 2014-11-05 대림산업 주식회사 폴리부텐의 제조 방법
KR101523568B1 (ko) * 2013-05-16 2015-05-28 대림산업 주식회사 반응성 폴리부텐 및 비반응성 폴리부텐의 선택적 제조장치 및 방법
KR20150005206A (ko) * 2013-07-05 2015-01-14 대림산업 주식회사 폴리부텐 제조 시 발생되는 폐수의 처리 장치 및 방법
KR102222524B1 (ko) * 2013-07-17 2021-03-03 바스프 에스이 측쇄 내의 비닐리덴 이중 결합의 백분율이 높은 고반응성 폴리이소부틸렌
KR101658545B1 (ko) 2014-08-22 2016-09-21 대림산업 주식회사 폴리부텐의 제조방법
KR101921891B1 (ko) 2015-07-02 2018-11-26 사우디 아라비안 오일 컴퍼니 프로필렌 제조용의 이중 촉매 시스템
WO2017003817A1 (fr) 2015-07-02 2017-01-05 Saudi Arabian Oil Company Systèmes et procédés de production de propylène
JP6605939B2 (ja) 2015-12-17 2019-11-13 Ｊｘｔｇエネルギー株式会社 ブテンポリマーの製造方法
WO2017151339A1 (fr) * 2016-03-03 2017-09-08 Tpc Group Llc Polyisobutylène réactif à faible teneur en fluorures
US10550048B2 (en) 2017-01-20 2020-02-04 Saudi Arabian Oil Company Multiple-stage catalyst system for self-metathesis with controlled isomerization and cracking
US10934231B2 (en) 2017-01-20 2021-03-02 Saudi Arabian Oil Company Multiple-stage catalyst systems and processes for propene production
US10329225B2 (en) * 2017-01-20 2019-06-25 Saudi Arabian Oil Company Dual catalyst processes and systems for propylene production
US10961171B2 (en) 2018-10-10 2021-03-30 Saudi Arabian Oil Company Catalysts systems that include metal co-catalysts for the production of propylene
US11242299B2 (en) 2018-10-10 2022-02-08 Saudi Arabian Oil Company Catalyst systems that include metal oxide co-catalysts for the production of propylene
KR102203006B1 (ko) * 2019-04-24 2021-01-13 대림산업 주식회사 고반응성 폴리부텐의 제조 방법
US11311869B2 (en) 2019-12-03 2022-04-26 Saudi Arabian Oil Company Methods of producing isomerization catalysts
US11517892B2 (en) 2019-12-03 2022-12-06 Saudi Arabian Oil Company Methods of producing isomerization catalysts
US11339332B2 (en) 2020-01-29 2022-05-24 Saudi Arabian Oil Company Systems and processes integrating fluidized catalytic cracking with metathesis for producing olefins
US11572516B2 (en) 2020-03-26 2023-02-07 Saudi Arabian Oil Company Systems and processes integrating steam cracking with dual catalyst metathesis for producing olefins
US11679378B2 (en) 2021-02-25 2023-06-20 Saudi Arabian Oil Company Methods of producing isomerization catalysts
US11845705B2 (en) 2021-08-17 2023-12-19 Saudi Arabian Oil Company Processes integrating hydrocarbon cracking with metathesis for producing propene

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2409727A (en) * 1942-01-30 1946-10-22 Phillips Petroleum Co Production of olefin polymers
DE2702604C2 (de) * 1977-01-22 1984-08-30 Basf Ag, 6700 Ludwigshafen Polyisobutene
DE2802198A1 (de) * 1978-01-19 1979-07-26 Basf Ag Verfahren zur gewinnung von isobuten aus isobuten enthaltenden c tief 4 -kohlenwasserstoffgemischen
NZ197347A (en) * 1980-06-12 1983-06-14 British Petroleum Co Dehydroisomerisation of n-butane to isobutene
GB2121431A (en) * 1982-06-08 1983-12-21 Exxon Research Engineering Co Isomerisation of butene-1 to butene-2 in isobutylene
US4436949A (en) * 1982-09-21 1984-03-13 Phillips Petroleum Company Olefin conversion process
US5043523A (en) * 1982-11-12 1991-08-27 Texas Petrochemicals Corporation Al2 O3 alkene isomerization process and catalyst
FI860203A (fi) * 1985-01-22 1986-07-23 Air Prod & Chem Dehydroisomerisering av kolvaeten.
BE1006694A5 (fr) * 1991-06-22 1994-11-22 Basf Ag Procede de preparation de polyisobutenes extremement reactifs.
GB9404368D0 (en) * 1994-03-07 1994-04-20 Bp Chem Int Ltd Production of polyisobutenes
US5811379A (en) * 1996-06-17 1998-09-22 Exxon Chemical Patents Inc. Polymers derived from olefins useful as lubricant and fuel oil additives, processes for preparation of such polymers and additives and use thereof (PT-1267)
FR2802921B1 (fr) * 1999-12-24 2002-08-23 Inst Francais Du Petrole Production d'isobutene de haute purete et de propylene a partir de coupes d'hydrocarbures a quatre atomes de carbone

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2007141277A1 *

Also Published As

Publication number Publication date
CN101460530A (zh) 2009-06-17
KR20090014372A (ko) 2009-02-10
WO2007141277A1 (fr) 2007-12-13
US20100234542A1 (en) 2010-09-16

Similar Documents

Publication Publication Date Title
EP2029638A1 (fr) Fabrication de polyisobutène réactif et sensiblement exempt d&#39;halogène à partir de mélanges d&#39;hydrocarbures en c4 pauvres en isobutène
DE69612423T2 (de) Verfahren und Einrichtung zur Umsetzung des olefinischen C4-Schnitts in Polyisobuten und Propylen
DE69707808T2 (de) Verfahren zur Herstellung von Isobuten und Propen aus Kohlenwasserstofffraktionen mit vier Kohlenstoffatomen
DE69816821T2 (de) Verbessertes Verfahren zur Herstellung von gesättigten Oligomeren
EP3599230B1 (fr) Procédé d&#39;oligomérisation des butènes par détermination du contenu d&#39;une catalyse acide
DE69428911T2 (de) Selektive hydrierung von hoch ungesättigten verbindungen in kohlenwasserstoffströmen
EP0628575B1 (fr) Procédé de préparation de polyisobutènes hautement réactifs
EP1989239B1 (fr) Procede de fabrication de polyisobutylene ayant une teneur en doubles liaisons terminales superieure a 50 % a partir d&#39;un courant technique d&#39;hydrocarbures en c4 contenant du 1-butene, du 2-butene et de l&#39;isobutene
DE112010004078T5 (de) Hydroisomerisierung und selektive hydrierung einer beschickung bei der durch ionische flüssigkeiten katalysierten alkylierung
EP1784476A1 (fr) Procede pour produire des aldehydes c5 et du propene a partir d&#39;un flux c4 contenant du 1-butene et du 2-butene
DE671419T1 (de) Herstellung von Polybutenen.
DE69502137T2 (de) Verfahren zur Methathesis von Olefinen
EP1117708B1 (fr) Procede de production de polyisobutene reactif exempt d&#39;halogene
DE3122078A1 (de) Als schmieroel verwendbare fluessigkeit, verfahren zu ihrer herstellung und ihre verwendung
WO2013120859A1 (fr) Complexe catalyseur au trifluorure de bore et procédé de production d&#39;homopolymères d&#39;isobutène hautement réactifs
DE1595154A1 (de) Verfahren zur Herstellung von Polymerisaten aus einer C?- bis C?-Kohlenwasserstoff-Fraktion
DE60029595T2 (de) Mittleres öl für dispersionsverfahren und verfahren zur herstellung von dimethylether
WO2013013856A1 (fr) Traitement final de mélanges d&#39;hydrocarbures en c4 contenant des oléfines
EP0900773B1 (fr) Procédé pour la préparation d&#39;alcènes à double liaison en bout de chaine
EP2802610B1 (fr) Procédé de production en continu de polyisobutylène
WO2015032804A1 (fr) Procédé de production de produits à base d&#39;hydrocarbures
DE2802199A1 (de) Verfahren zur gewinnung von isobuten aus isobuten enthaltenden c tief 4 -kohlenwasserstoffgemischen
DE2005207C3 (de) Verfahren zur Herstellung von Polybutenölen mit erhöhter Viskosität
DE3049213A1 (de) Verfahren zur gemeinsamen herstellung von alkyl-tert.-butylether und gewinnung von butadien
EP2995599A1 (fr) Procédé et système de fabrication d&#39;hydrocarbures

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20090107

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LI LT LU LV MC MT NL PL PT RO SE SI SK TR

AX Request for extension of the european patent

Extension state: AL BA HR MK RS

17Q First examination report despatched

Effective date: 20090402

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20101019