EP1478609A2 - Procede modifie de production d'alcools tensioactifs et d'ethers d'alcools tensioactifs, produits ainsi obtenus et leur utilisation - Google Patents

Procede modifie de production d'alcools tensioactifs et d'ethers d'alcools tensioactifs, produits ainsi obtenus et leur utilisation

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Publication number
EP1478609A2
EP1478609A2 EP03706531A EP03706531A EP1478609A2 EP 1478609 A2 EP1478609 A2 EP 1478609A2 EP 03706531 A EP03706531 A EP 03706531A EP 03706531 A EP03706531 A EP 03706531A EP 1478609 A2 EP1478609 A2 EP 1478609A2
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EP
European Patent Office
Prior art keywords
olefin
mixture
butene
olefins
surfactant
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EP03706531A
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German (de)
English (en)
Inventor
Michael Röper
Jürgen STEPHAN
Götz-Peter SCHINDLER
Jürgen Tropsch
Thomas Heidemann
Martina Prinz
Soeren Zimdahl
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BASF SE
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BASF SE
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
    • C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
    • C07C29/14—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group
    • C07C29/141—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group with hydrogen or hydrogen-containing gases
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/02—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons
    • C07C2/04—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation
    • C07C2/06—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation of alkenes, i.e. acyclic hydrocarbons having only one carbon-to-carbon double bond
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/03—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by addition of hydroxy groups to unsaturated carbon-to-carbon bonds, e.g. with the aid of H2O2
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/16—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxo-reaction combined with reduction
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/49—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide
    • C07C45/50—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide by oxo-reactions
    • 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

Definitions

  • the present invention relates to a process for the preparation of surfactant alcohols and surfactant alcohol ethers, which are very suitable, inter alia, as surfactants or for the preparation of surfactants.
  • a metathesis reaction produces olefins or olefin mixtures which are dimerized to form an olefin mixture having 10 to 16 carbon atoms which contains less than 10% by weight of compounds which have a vinylidene group which
  • the olefins are then derivatized to surfactant alcohols and optionally alkoxylated.
  • the C 4 olefins are prepared as described in the present application.
  • the invention further relates to the use of the surfactant alcohols and surfactant alcohol ethers for the production of surfactants by glycosidation or polyglycosidation, sulfation or phosphatization.
  • Fatty alcohols with chain lengths from C 8 to C 18 are used for the production of nonionic surfactants. These are reacted with alkylene oxides to give the corresponding fatty alcohol ethoxylates. (Chapter 2.3 in: Kosswig / Stache, "Die Tenside”, Carl Hanser Verlag, Kunststoff Vienna (1993)).
  • the chain length of the fatty alcohol influences different tenside properties such as wetting, foaming, fat dissolving, cleaning power.
  • Fatty alcohols with chain lengths from C 8 to Cj 8 can also be used for the production of anionic surfactants, such as alkyl phosphates and alkyl ether phosphates. Instead of phosphates, the corresponding sulfates can also be produced. (Chapter 2.2 in: Kosswig / Stache, "Die Tenside", Carl Hanser Verlag, Kunststoff Vienna (1993)). Such fatty alcohols can be obtained from native sources, for example from fats and oils, or by synthetic means from building blocks with a lower number of carbon atoms. A variant is the dimerization of an olefin to a product with double the number of carbon atoms and its functionalization to an alcohol.
  • a number of processes are known for dimerizing olefins.
  • the reaction can be carried out on a heterogeneous cobalt oxide / carbon catalyst (DE-Al 468 334), in the presence of acids such as sulfuric or phosphoric acid (FR 964 922), aluminum alkyl-catalyzed (WO 97/16398), or with a dissolved nickel complex catalyst (US-A-4 069 273).
  • acids such as sulfuric or phosphoric acid
  • FR 964 922 aluminum alkyl-catalyzed
  • a dissolved nickel complex catalyst US-A-4 069 273
  • 1,5-cyclooctadiene or 1,1,1,5,5,5,5 hexafluoropentane-2,4-dione are used as complexing agents - Highly linear olefins with a high proportion of dimerization products.
  • the functionalization of the olefins to form alcohols by building up the carbon skeleton around a carbon atom is advantageously carried out via the hydroformylation reaction, which provides a mixture of aldehydes and alcohols, which can subsequently be hydrogenated to alcohols. Every year, around 7 million tons of products are manufactured worldwide using the hydroformylation of olefins.
  • An overview of catalysts and reaction conditions of the hydrofonnylation process is given, for example, by Beller et al. in Journal of Molecular Catalysis, AI 04 (1995), 17-85 or also Ullmanns Encyclopedia of Industrial Chemistry, Vol. A5 (1986), page 217 ff, page 333, as well as the relevant references.
  • sulfates, alkoxylates, alkoxysulfates and carboxylates of a mixture of branched alkanols (oxo alcohols) show good surface activity in cold water and have good biodegradability.
  • the alkanols of the mixture used have a chain length of more than 8 carbon atoms, they have an average of 0.7 to 3 branches on the Alkanol mixtures can be prepared, for example by hydroformylation, from mixtures of branched olefins, which in turn can be obtained either by skeletal isomerization or by dimerization of internal, linear olefins.
  • Another disadvantage of this known process is the use of mixtures of internal olefins which are required for the production of branched surfactant oxo alcohols and which are only accessible by isomerization of alpha olefins. Such processes always lead to isomer mixtures which, due to the different physical and chemical data of the components, are more difficult to handle than pure substances. In addition, the additional process step of isomerization is required, which means that the process has a further disadvantage.
  • the structure of the components of the oxo-alkanol mixture depends on the type of olefin mixture which has been subjected to the hydroformylation. Olefin mixtures obtained from skeletal isomerization from alpha olefin mixtures lead to alkanols which are predominantly branched at the ends of the main chain, ie in positions 2 and 3, calculated from the respective chain end (page 56, last paragraph).
  • oxo alcohols are obtained by the process disclosed in this publication, the branches of which lie more in the middle of the main chain, as shown in Table IV on page 68, largely at C4 and more distant carbon atoms based on the hydroxyl carbon atom. On the C2 and C3 Positions relative to the hydroxyl carbon atom, on the other hand, are less than 25% of the branches (pages 28/29 of this document).
  • the surface-active end products are obtained from the alkanol mixtures either by oxidizing the -CH 2 OH group to the carboxyl group, or by sulfating the alkanols or their alkoxylates.
  • the vinylidene compounds are then double bond isomerized, so that the double bond migrates further from the chain end to the center and then subjected to the hydroformylation to give an oxo alcohol mixture.
  • This is then further converted to surfactants, for example by sulfation.
  • a serious disadvantage of this process is that it starts from alpha olefins.
  • Alpha olefins are obtained, for example, by transition metal-catalyzed oligomerization of ethylene, Ziegler build-up reaction, wax cracking or Fischer-Tropsch processes and are therefore relatively expensive starting materials for the preparation of surfactants.
  • Another significant disadvantage of this known surfactant production process is that there is a gap between it the dimerization of the alpha olefins and the hydroformylation of the Dimerization product a skeletal isomerization must be switched on if you want to come to predominantly branched products. Because of the use of a relatively expensive starting material for the production of surfactants and the need to switch on an additional process step, the isomerization, this known process is economically considerably disadvantaged.
  • WO 00/39058 describes that for the production of branched olefins and alcohols (oxo alcohols) which can be further processed to very effective surfactants - hereinafter referred to as "surfactant alcohols" - neither on alpha olefins nor on olefins, which are mainly have been prepared from ethylene, but that inexpensive C 4 -olefin streams can be used and that the isomerization step can also be avoided if the process described in this document is used.
  • surfactant alcohols neither on alpha olefins nor on olefins, which are mainly have been prepared from ethylene, but that inexpensive C 4 -olefin streams can be used and that the isomerization step can also be avoided if the process described in this document is used.
  • a process for the production of surfactant alcohols and surfactant alcohol ethers is disclosed by derivatizing olefins having about 10 to 20 carbon atoms or mixtures of such olefins and optionally subsequent alkoxylation, characterized in that a) subjecting a C 4 -olefin mixture to metathesis, b ) separating olefins with 5 to 8 carbon atoms from the metathesis mixture, c) subjecting the separated olefins individually or in a mixture to dimerization to olefin mixtures with 10 to 16 carbon atoms, d) subjecting the olefin mixture obtained to derivatization, if appropriate after fractionation subject to a mixture of surfactant alcohols and e) optionally alkoxylating the surfactant alcohols.
  • the C 4 -olefin streams used here are mixtures which consist essentially, preferably to over 80 to 85% by volume, in particular over 98% by volume, of 1-butene and 2-butene, and to a lesser extent - usually not more than 15 to 20 Vol .-% - n-butane and isobutane in addition to traces of polyunsaturated C 4 hydrocarbons and Cs hydrocarbons.
  • These hydrocarbon mixtures also referred to in technical terms as "raffinate II" are produced as a by-product in the cracking of high-molecular hydrocarbons, for example crude oil.
  • the low molecular weight olefins, ethene and propene produced in this process are renowned raw materials for the production of polyethylene and polypropylene, the hydrostatic fractions above C 6 are used as fuels in internal combustion engines and for heating purposes.
  • WO 00/39058 is only suitable in the strict sense for the processing of so-called raffinate II.
  • Raffinate II is obtained by splitting higher molecular weight hydrocarbons, for example naphtha or gas oil.
  • C 4 mixtures which are obtained from other sources are also suitable as a starting product for the metathesis reaction described in WO 00/39058 and followed by the further implementation steps.
  • the dehydrogenation of butanes is a suitable C-olefin source. This method, which is known per se, is described, for example, in US Pat. No. 4,788,371, WO 94/29021, US Pat. No.
  • MTO process methanol to olefin
  • methanol is used on suitable zeolitic Catalysts converted to olefins.
  • the methanol is optionally produced from Cl hydrocarbons.
  • the MTO process is described, for example, in Weissermel, Arpe, Industrielle Organische Chemie, 5th edition 1998, pages 36 to 38.
  • Suitable methane mixtures of propene (Phillips Triolefin Process), the Fischer Tropsch process, or ethylene dimerization can also be used to obtain suitable C-olefin mixtures, as well as partial hydrogenation of butadiene.
  • surfactant alcohols are produced in the manner described in WO 00/39058 from a wide variety of C 4 -olefin mixtures (which in principle can originate from all of the abovementioned processes, in particular the olefin mixture raffinate II), the challenge of a different method of preparation arises process.
  • WO 00/39058 makes no statement as to which composition the raffinate II used should have. In particular, no indication is given regarding the required butene-1 / butene-2 ratio in such a raffinate. In the example that describes the metathesis of raffinate II, this has a butene-1 / butene-2 ratio of 1.06. It can be concluded from this that, in the process according to WO 00/39058, the metathesis stage a) can be carried out with a raffinate II in any desired composition that occurs in the usual industrial production processes.
  • EP-A-0 742 195 relates to a process for converting C 4 or C 5 cuts into ether and propylene.
  • diolefins are initially contained and selectively hydrogenating acetylenic impurities, the hydrogenation being associated with isomerization of 1-butene to 2-butene.
  • the yield of 2-butenes should be maximized.
  • the ratio of 2-butene to 1-butene is about 9: 1 after the hydrogenation.
  • This is followed by etherification of the isoolefins present, the ethers being separated from the C 4 cut . Oxygenate impurities are then removed.
  • the discharge obtained which mainly contains 2-butene in addition to alkanes, is then reacted with ethylene in the presence of a metathesis catalyst in order to obtain a reaction discharge which contains propylene as the product.
  • the metathesis is carried out in the presence of a catalyst which contains supported rhenium oxide.
  • DE-A-198 13 720 relates to a process for the production of propene from a C 4 stream.
  • DE-A-199 32 060 relates to a process for the preparation of C 5 - / C 6 -olefins by reacting a starting stream which contains 1-butene, 2-butene and isobutene in a metathesis to form a mixture of C 2-6 olefins.
  • propene in particular is obtained from butenes.
  • witches and methylpentene are removed as products.
  • No ethene is added in the metathesis.
  • ethene formed in the metathesis is returned to the reactor.
  • DE-A 100 13 537 discloses a process for the production of propene and hexene from an olefinic C 4 -hydrocarbon-containing raffinate II starting stream, in which
  • a metathesis reaction is carried out, in the context of which butenes contained in the starting stream with ethene to give an ethene, propene, butenes , 2- A mixture containing pentene, 3-hexene and butanes is reacted, using 0.05 to 0.6 molar equivalents of ethene, based on the butenes, b) the discharge stream thus obtained is first separated by distillation into a low-boiler fraction A containing C -C 3 olefins and in a high boiler fraction containing C 4 -C 6 olefins and butanes, c) the low boiler fraction A obtained from b) is then separated by distillation into a fraction containing ethene and a fraction containing propene, the fraction containing eth
  • the object of the present invention is to provide a process for the preparation of surfactant alcohols in accordance with the teaching of WO 00/39058, which makes it possible, in the production of 2-pentene and in particular 3-hexes, by metathesis and subsequent dimerization to provide a favorable product spectrum with regard to both To get olefins as well as the by-product distribution ideally, even without having to resort to the addition of large amounts of ethylene.
  • This is intended to improve the added value of surfactant alcohol synthesis, in particular by maintaining a valuable range of by-products.
  • This object is achieved by a process for the preparation of surfactant alcohols and surfactant alcohol ethers by derivatization of olefins having about 10 to 20 carbon atoms or mixtures of such olefins and optionally subsequent alkoxylation, in which process a) a C -olefin mixture with a Ratio of 1-butene / 2-butene of> 1.2 one
  • Subjects subject to metathesis b) separating olefins having 5 to 8 carbon atoms from the metathesis mixture, c) subjecting the separated olefins individually or in a mixture to dimerization to olefin mixtures having 10 to 16 carbon atoms, d) the olefin mixture obtained, optionally after fractionation , the
  • the process according to the invention manages, particularly when a 1-butene / 2-butene ratio is close to the ideal value of about 2, without the addition of ethylene.
  • 1-butene / 2-butene ratios close to the lower limit of 1.2 a favorable range of valuable products can still be obtained (formation of propene).
  • the external mass balance of the process can be influenced in a targeted manner by shifting the equilibrium by recycling certain partial flows.
  • the 3-hexene yield is increased in that the cross-metathesis of 1-butene with 2-butene is suppressed by recycling 2-pentene to the metathesis step, so that little or no 1-butene is consumed here.
  • ethene is additionally formed, which reacts in a subsequent reaction with 2-butene to give the valuable product propene.
  • Another surprising advantage of the process according to the invention is that the catalyst cycle times in the metathesis reaction are significantly extended compared to a process which cannot do without the addition of particularly large amounts of ethylene during the metathesis.
  • This advantage of the method according to the invention is particularly pronounced when only small amounts or no ethylene are added.
  • the catalyst cycle times in the process according to the invention are significantly extended compared to the processes of the prior art. In some cases up to 100% longer cycle times could be observed.
  • Olefin mixtures which contain 1-butene and 2-butene and optionally isobutene and can be used in the process according to the invention are obtained, inter alia, as a C fraction in various cracking processes such as steam cracking or FCC cracking.
  • butene mixtures such as those obtained in the dehydrogenation of butanes or by dimerization of ethene, can be used.
  • LPG, LNG or MTO flows can also be used.
  • Butanes contained in the C 4 fraction are inert.
  • dienes, alkynes or enynes are removed using conventional methods, such as extraction or selective hydrogenation, to remove harmless residual amounts.
  • the butene content of the C 4 fraction used in the process is 1 to 100% by weight, preferably 60 to 90% by weight.
  • the butene content relates to 1-butene, 2-butene and isobutene.
  • a C 4 fraction is thus used, such as is obtained in steam or FCC cracking or in the dehydrogenation of butane.
  • a C -olefin mixture can be produced from LPG, LNG or MTO streams.
  • the olefins are preferably obtained by dehydrogenation of the C 4 portion of the LPG stream and subsequent removal of any dienes, alkynes and enynes formed, the C 4 portion of the LPG stream before or after the dehydrogenation or removal of dienes, alkynes and enines is separated from the LPG stream.
  • an LNG stream is used, it is preferably converted into the C 4 -olefin mixture using an MTO process.
  • LPG 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 produced in oil refineries as by-products in the distillation and cracking of petroleum and in gas processing for gasoline 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 By low-temperature or pressure distillation, the field butanes are obtained, the composition of which varies depending on the deposit, but which generally contain about 30% isobutane and about 65% n-butane.
  • the C 4 -olefin mixtures used for the production of surfactant alcohols according to the invention can be obtained in a suitable manner by separating off the C component and dehydrating and feed cleaning.
  • Possible working-up sequences for LPG or LNG streams are dehydrogenation, subsequently separation or partial hydrogenation of the dienes, alkynes and enynes and subsequently isolation of the C -olefins.
  • the dehydrogenation can be followed first by the isolation of the C 4 olefins, followed by the removal or partial hydrogenation of the dienes, alkynes and enines and, if appropriate, further by-products.
  • the dehydrogenation can, for example, be carried out in a heterogeneously catalyzed manner in one or more reaction zones, at least some of the heat of dehydrogenation required being generated in at least one reaction zone by burning hydrogen, the hydrocarbon or hydrocarbons and / or carbon in the presence of an oxygen-containing gas directly in the reaction mixture ,
  • 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 ZrO 2 , SiO 2 , ZrO 2 / SiO 2 , ZrO 2 / SiO 2 / Al 2 O 3 , Al 2 O 3 , Mg (Al) O.
  • 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 -olefm mixture using an MTO process.
  • MTO stands for methanol-to-olefin. It is related to the MTG (Methanol-To-Gasoline) process. It is a process for the dehydration of methanol over a suitable catalyst, whereby an olefinic hydrocarbon mixture is formed.
  • CrFeed current methanol synthesis can be carried out using the MTO process.
  • CrFeed streams can thus be converted into olefin mixtures from methanol and the MTO process, from which the C 4 olefins can be separated off by suitable methods. The separation can take place, for example, by distillation.
  • MTO MTO
  • the methanol-to-olefin process is also described, for example, in PJ Jackson, N. White, Technologies for the Conversion of Natural Gas, Austr. Inst. Energy Conference 1985.
  • the C 4 -olefin mixtures can also be prepared by methathesis of propene (Phillipps Triolefin Process). The methathesis can be carried out as described in the present application.
  • the C -olefin mixtures can be obtained by a Fischer-Tropsch process (gas to liquid) or by ethene dimerization. Suitable methods are described in the previously cited book by Weissermel and Arpe on pages 23 ff. And 74 ff.
  • butanes present are separated off by the customary measures known to the person skilled in the art, for example by distillation, selective extraction or extractive distillation.
  • isobutane can be separated off by distillation.
  • the conventional solvents known to those skilled in the art are used in selective extraction and extractive distillation, for example N-methylpyrrolidone (NMP).
  • the sub-step selective hydrogenation of butadiene and acetylenic impurities contained in the crude C 4 fraction is preferably carried out in two stages
  • Carrier contains, preferably palladium on alumina, at a temperature of 20 to 200 ° C, a pressure of 1 to 50 bar, a volume velocity of 0.5 to 30 m of fresh feed per m of catalyst per hour and a ratio of recycle to
  • 1-butene and 2-butene are present in a molar ratio of> 1.2, preferably> 1.4, more preferably> 1.8 and in particular about 2. It preferably contains essentially no diolefins and acetylenic compounds.
  • 1-butene is preferably present in excess in the above-mentioned 1-butene / 2-butene ratio of> 1.2, preferably> 1.4, in particular> 1.8.
  • the optimum is at the above-mentioned ratio of 1-butene / 2-butene of about 2.
  • butene mixtures can also be used in which the molar ratio of 1-butene / 2-butene is at even higher, arbitrary values. However, with a ratio of 2, the best product distribution results.
  • the sub-step butadiene extraction from crude C section is preferably carried out with a butadiene-selective solvent, selected from the class of polar aprotic solvents, such as acetone, furfural, acetonitrile, dimethylacetamide, dimethylformamide and N-methylpyrrolidone, in order to obtain a reaction discharge , in which the n-butenes 1-butene and 2-butene are present in a molar ratio of 2: 1 to 1:10, preferably from 2: 1 to 1: 2.
  • a butadiene-selective solvent selected from the class of polar aprotic solvents, such as acetone, furfural, acetonitrile, dimethylacetamide, dimethylformamide and N-methylpyrrolidone
  • the substep isobutene etherification is preferably carried out in a three-stage reactor cascade with methanol or isobutanol, preferably isobutanol in the presence of an acidic ion exchanger, in which flooded fixed bed catalysts are flowed through from top to bottom, the reactor inlet temperature being 0 to 60 ° C., preferably 10 to 50 ° C, the initial temperature 25 to 85 ° C, preferably 35 to 75 ° C, the pressure 2 to 50 bar, preferably 3 to 20 bar and the ratio of isobutanol to isobutene 0.8 to 2.0, preferably 1.0 is up to 1.5 and the total turnover corresponds to the equilibrium turnover.
  • the substep isobutene separation is preferably carried out by oligomerization or polymerization of isobutene, starting from the reaction discharge obtained after the butadiene extraction and / or selective hydrogenation steps described above, in the presence of a catalyst which is selected from the class of homogeneous and heterogeneous Broensted acids, preferably from heterogeneous contacts which contain an oxide of a metal from sub-group B of the Periodic Table of the Elements, even with an acidic inorganic support, particularly preferably WO 3 / TiO 2 , in order to generate a current which has less than 15% residual isobutene ,
  • the C 4 stream of a steam cracker contains a high proportion of polyunsaturated compounds such as 1,3-butadiene, 1-butyne (ethyl acetylene) and butenine (vinyl acetylene).
  • polyunsaturated compounds such as 1,3-butadiene, 1-butyne (ethyl acetylene) and butenine (vinyl acetylene).
  • the polyunsaturated compounds are either extracted (butadiene extraction) or selectively hydrogenated.
  • the residual content of polyunsaturated compounds is typically 0.05 to 0.3% by weight, in the latter case typically 0.1 to 4.0% by weight. Since the remaining amounts of polyunsaturated compounds also interfere with further processing, further enrichment by selective hydrogenation to values ⁇ 10 ppm is required. In order to obtain the highest possible product value of butenes, the overhydrogenation to butanes must be kept as low as possible.
  • bimetallic catalysts for selective hydrogenation of C 2 -, C 3 -, C 4 -, C 5 - and C 5+ -hydrocarbon streams.
  • bimetallic catalysts made from Gp.VIII and Gp.IB metals show improvements in selectivity compared to pure Pd supported catalysts.
  • the catalyst is characterized in that the alumina carrier with BET 120 m 2 / g is first subjected to a steam treatment at 110-300 ° C and then calcined at 500-1200 ° C. Finally, the Pd compound is applied and calcined at 300-600 ° C.
  • Catalyst which consists among other things of Pd and In or Ga on a carrier.
  • the catalyst combination enables use without CO addition with high activity and selectivity.
  • the catalyst preparation comprises the following steps:
  • Catalyst consisting of Pd and Ag and alkali fluoride on an inorganic support.
  • Catalyst is characterized in that the active component is predominantly in the meso and macro pores.
  • the catalyst is further characterized by a large pore volume and low vibrating weight. So the catalyst has
  • Example 1 a vibrating weight of 383 g / 1 and a pore volume of 1.17 ml / g.
  • the preferred catalyst consists of
  • Catalyst made of Pd and at least one alkali fluoride and optionally Ag on an inorganic support (Al 2 O 3 , TiO 2 and / or ZrO 2 ).
  • the catalyst combination enables selective hydrogenation in the presence of sulfur compounds.
  • Catalyst based on noble metal and / or ethene oxide on Al O 3 supports with a defined X-ray diffraction pattern.
  • the carrier consists of n-Al 2 O 3 and / or ⁇ -Al O 3 . Due to the special support, the catalyst has a high initial selectivity and can therefore be used immediately for the selective hydrogenation of unsaturated compounds.
  • Another electron donor is also used. This consists of either containing N-from 'a-deposited on the catalyst metal, such as Na, K, Ag, Cu, Ga, In, Cr, Mo or La, or an addition to the hydrocarbon feedstock, such as alcohol, ether, or compounds ,
  • the measures mentioned can reduce the 1-butene isomerization.
  • the catalyst is primarily used for the hydrogenation of low-butadiene hydrocarbon streams.
  • IB metal on an Al 2 O 3 support with at least 80% of the Pd and 80% of the Gp.
  • the simplified principle of a solvent extraction from crude C 4 section can be represented as follows:
  • the completely evaporated C 4 section is fed to an extraction column at the lower end.
  • the solvent (DMF, NMP) flows towards the gas mixture from above and is loaded with more soluble butadiene and small amounts of butenes on the way down.
  • Part of the pure butadiene obtained is fed in at the lower end of the extraction column in order to largely drive off the butenes.
  • the butenes leave the column at the head.
  • outgas the butadiene is freed from the solvent by boiling and then pure distilled.
  • the reaction product from an extractive butadiene distillation is usually fed into the second stage of a selective hydrogenation in order to reduce the residual butadiene content to values of ⁇ 10 ppm.
  • C 4 raffinate or raffinate I The C stream remaining after removal of butadiene is referred to as C 4 raffinate or raffinate I and mainly contains the components isobutene, 1-butene, 2-butenes and n- and isobutanes.
  • isobutene is preferably isolated subsequently, since it is distinguished from the others by its branching and its higher reactivity C components differs.
  • shape-selective molecular sieve separation with which isobutene can be obtained with a purity of 99% and n-butenes and butane adsorbed on the molecular sieve pores can be desorbed again using a higher-boiling hydrocarbon, this is done primarily by distillation using a so-called deisobutenizer , with which isobutene is removed together with 1-butene and isobutene overhead and 2-butenes and n-butane including residual amounts of iso- and 1-butene remain in the bottom, or extractive by reacting isobutene with alcohols on acidic ion exchangers.
  • methanol (MTBE) or isobutanol (IBTBE) are preferably used.
  • MTBE is produced from methanol and isobutene at 30 to 100 ° C and slightly overpressure in the liquid phase on acidic ion exchangers.
  • the pressure-dependent azeotrope formation between methanol and MTBE requires a multi-stage pressure distillation in order to reproduce MTBE or is achieved by newer technology through methanol adsorption on adsorber resins. All other components of the C 4 fraction remain unchanged.
  • bifunctional PD-containing ion exchangers are preferably used, in which only diolefins and acetylenes are hydrogenated in the presence of small amounts of hydrogen. The etherification of the isobutene remains unaffected.
  • MTBE is primarily used to increase the octane number of gasoline.
  • MTBE and IBTBE can be cleaved on acidic oxides in the gas phase at 150 to 300 ° C for the pure recovery of isobutene.
  • guard bed to remove catalyst poisons, such as water, oxygenates, sulfur or sulfur compounds or organic halides.
  • butadiene (1,2- and 1,3-butadiene) and alkynes or alkenins contained in the C 4 cut are selectively hydrogenated in a two-stage process.
  • the C stream originating from the refinery can also be fed directly into the second step of the selective hydrogenation.
  • the first step of the hydrogenation is preferably carried out on a catalyst which contains 0.1 to 0.5% by weight of palladium on aluminum oxide as a support.
  • the reaction is carried out in the gas / liquid phase in a fixed bed (trickle mode) with a liquid circuit.
  • the hydrogenation takes place at a temperature in the range from 40 to 80 ° C. and a pressure of 10 to 30 bar, a molar ratio of hydrogen to butadiene from 10 to 50 and a volume velocity LHSV of up to 15 m 3 fresh feed per m 3 catalyst per hour and one Ratio of recycle of inflow operated from 5 to 20.
  • the second step of the hydrogenation is preferably carried out on a catalyst which contains 0.1 to 0.5% by weight of palladium on aluminum oxide as a support.
  • the reaction is carried out in the gas / liquid phase in a fixed bed (trickle mode) with a liquid cycle.
  • the hydrogenation takes place at a temperature in the range from 50 to 90 ° C. and a pressure from 10 to 30 bar, a molar ratio of hydrogen to butadiene from 1.0 to 10 and a volume velocity LHSV from 5 to 20 m 3 fresh feed per m 3 catalyst operated per hour and a recycle to inflow ratio of 0 to 15.
  • the residual butadiene content can be 0 to 50 ppm, depending on the degree of hydrogenation.
  • the reaction product obtained in this way is referred to as raffinate I and, in addition to isobutene, has 1-butene and 2-butene in different molar ratios.
  • the extraction of butadiene from crude C 4 cuts is preferably carried out using BASF technology using N-methylpyrrolidone.
  • the reaction discharge from the extraction is fed into the second step of the selective hydrogenation described above in order to remove residual amounts of butadiene, care being taken to ensure that isomerization of 1-butene to 2-butene is nonexistent or only slight.
  • etherification stage isobutene is reacted with alcohols, preferably with isobutanol, over an acidic catalyst, preferably over an acidic ion exchanger, to give ether, preferably isobutyl tert-butyl ether.
  • the reaction takes place in a three-stage reactor cascade in which flooded fixed bed catalysts are flowed through from top to bottom.
  • the inlet temperature 0 to 60 ° C, preferably 10 to 50 ° C; the initial temperature is between 25 and 85 ° C, preferably between 35 and 75 ° C, and the pressure is 2 to 50 bar, preferably 3 to 20 bar.
  • a ratio of isobutanol to isobutene of 0.8 to 2.0, preferably 1.0 to 1.5, the conversion is between 70 and 90%.
  • the inlet temperature is 0 to 60 ° C, preferably 10 to 50 ° C; the starting temperature is between 25 and 85, preferably between 35 and 75 ° C., and the pressure is 2 to 50 bar, preferably 3 to 20 bar.
  • the total conversion over the two stages increases to 85 to 99%, preferably 90 to 97%.
  • the equilibrium turnover achieved In the third and largest reactor at the same inlet and outlet temperature from 0 to 60 ° C, preferably 10 to 50 ° C; the equilibrium turnover achieved.
  • the ether cleavage follows the etherification and separation of the ether formed: the endothermic reaction is carried out on acidic catalysts, preferably on acidic heterogeneous contacts, for example phosphoric acid on an SiO 2 support , at an inlet temperature of 150 to 300 ° C., preferably at 200 to 250 ° C, and an initial temperature of 100 to 250 ° C, preferably at 130 to 220 ° C.
  • raffinate II The reaction discharge obtained in this way, referred to as raffinate II, has a residual isobutene content of 0.1 to 3% by weight.
  • the remaining raffinate stream can be prepared by distillation according to one embodiment of the invention before further processing. Purification of the raffinate II stream on adsorber materials
  • the raffinate fl stream obtained after the etherification / polymerization (or distillation) is purified on at least one protective bed consisting of high-surface area aluminum oxides, silica gels, aluminum silicates or molecular sieves.
  • the protective bed serves to dry the C 4 stream and to remove substances which can act as a catalyst poison in the subsequent metathesis step.
  • the preferred adsorbent materials are Selexsorb CD and CDO as well as 3A and NaX molecular sieves (13X). Cleaning takes place in drying towers at temperatures and pressures that are selected so that all components are in the liquid phase. If necessary, the feed preheating cleaning step is used for the subsequent metathesis step.
  • the remaining raffinate II stream is almost free of water, oxygenates, organic chlorides and sulfur compounds.
  • the etherification step is carried out with methanol to produce MTBE, it may be necessary to combine several purification steps or to connect them in series due to the formation of dimethyl ether as a secondary component.
  • compositions of C4-olefin streams are given below which are obtained in the customary processes mentioned in the description and which, if appropriate after enrichment by distillation or catalytic distillation to the desired ratio of 1-butene / 2-butene, as a starting material stream in the process according to the invention Procedures can be used.
  • the stream to be used according to the invention in the metathesis does not have the desired 1-butene / 2-butene ratio
  • the stream can be enriched with 1-butene by measures known to the person skilled in the art.
  • a preferred enrichment method is distillation.
  • the main constituents still present in the C stream can be separated from one another by distillation, or fractions can be obtained by distillation which are enriched with one or more components.
  • the boiling points of the main and secondary components at 101.3 kPa are given in the table below.
  • a raffinate II which has the usual composition and contains the above-mentioned components in different concentrations, is subjected to distillation, isobutane is obtained as the top product.
  • the middle distilate contains 1-butene (contaminated with isobutene), while the bottom contains mainly n-butane, trans-2-butene and cis-2-butene.
  • the separation of the C4 stream or the enrichment with 1-butene can be carried out in two columns.
  • the enrichment can preferably be carried out by a combination of catalytic isomerization and distillative separation of the C stream used.
  • 1-butene can be separated from the C 4 mixture by distillation. If the remaining mixture can isomerize by the presence of a catalyst, new 1-butene always forms from 2-butene as a result of the removal of 1-butene from the equilibrium.
  • Such a process can be carried out in two stages, that is, by carrying out the isomerization and distillation in different process units. It is also possible to carry out isomerizing distillation in a single process unit (catalytic distillation).
  • the isomerization catalyst is located in the distillation column or in the distillation bottoms.
  • the isomerization catalysts used are known to the person skilled in the art. They generally contain elements of groups Ia, Ha, fllb, IVb, Vb or VIII. Of the periodic table of the elements.
  • heterogeneous or homogeneous catalysts containing RuO 2 , MgO, CaO, ZnO, Rb / Cs / K on Al 2 O 3 , Na on Al 2 O 3 , K 2 CO 3 , Na 2 CO 3 , PD / Al 2 O 3 , PdO, boron halides (e.g.
  • BC1 3 BC1 3 , BF 3 , basic Al 2 O 3 , oxides of the lanthanide group La 2 O 3 , Nd 2 O 3 , NiO mixed catalysts, TiO 2 , ZrO 2 , C 2 O, KC 8 , Rb 2 O, KF / Al 2 O 3 , tungsten silicic acid, Co on activated carbon, acidic zeolites, acidic ion exchangers, Co (acac) 2 , Fe (CO) 5 , Ru 2+ (H 2 O) 6 in EtOH, Rh 3+ complexes ,
  • Al 2 O 3 , SiO 2 or activated carbon for example, can be used as catalyst supports for heterogeneous systems.
  • olefins having 5 to 10 C atoms, preferably 5 to 8 C atoms, but especially pentene, are used in the presence of suitable catalysts -2 and hexene-3 formed.
  • Suitable catalysts are preferably molybdenum, tungsten or rhenium compounds. It is particularly expedient to carry out the reaction under heterogeneous catalysis, the catalytically active metals being used in particular in conjunction with supports made of Al 2 O 3 or SiO 2 . Examples of such catalysts are MoO 3 or WO 3 on SiO 2 , or Re 2 O 7 on Al 2 O 3 .
  • the metathesis reaction is preferably carried out in the presence of heterogeneous, not or only slightly isomerization-active metathesis catalysts which are selected from the class of transition metal compounds of metals from group VI, VIII.b or VIII. Of the Periodic Table of the Elements applied to inorganic supports.
  • Rhenium oxide on a support preferably on ⁇ -aluminum oxide or on Al 2 O 3 / B 2 O 3 / SiO 2 mixed supports, is preferably used as the metathesis catalyst.
  • the catalyst used is Re 2 O 7 / ⁇ -Al 2 O 3 with a rhenium oxide content of 1 to 20%, preferably 3 to 15%, particularly preferably 6 to 12% by weight.
  • the metathesis can be carried out in the liquid phase or preferably in the gas phase.
  • the metathesis is preferably carried out at a temperature of 0 to 150 ° C., particularly preferably 20 to 80 ° C. and a pressure of 2 to 200 bar, particularly preferably 5 to 30 bar.
  • the temperature is preferably 20 to 300 ° C., particularly preferably 50 to 200 ° C.
  • the pressure is preferably 1 to 20 bar, particularly preferably 1 to 5 bar.
  • the metathesis can be carried out in the presence of a rhenium catalyst, since in this case particularly mild reaction conditions are possible.
  • the metathesis can be carried out at a temperature of 0 to 50 ° C and at low pressures of approx. 0.1 to 0.2 MPa.
  • the dimerization of the olefins or olefin mixtures obtained in the metathesis step gives dimerization products which have particularly favorable components and a particularly advantageous composition with regard to the further processing on surfactant alcohols if a dimerization catalyst is used which contains at least one element of subgroup VIII of the periodic system of the elements, and the catalyst composition and the reaction conditions are selected so that a dimer mixture is obtained which contains less than 10% by weight of compounds which contain a structural element of the formula I (vinylidene group)
  • a 1 and A 2 are aliphatic hydrocarbon esters.
  • the internal linear pentenes and hexenes contained in the metathesis product are preferably used for the dimerization.
  • the use of 3-hexes is particularly preferred.
  • the dimerization can be carried out homogeneously or heterogeneously.
  • the heterogeneous procedure is preferred, since on the one hand the catalyst separation is simplified and the process is therefore more economical, and on the other hand no environmentally harmful wastewater is generated, as is usually the case when separating dissolved catalysts, for example by hydrolysis.
  • Another advantage of the heterogeneous process is that the dimerization product contains no halogens, especially chlorine or fluorine.
  • Homogeneously soluble catalysts generally contain halide-containing ligands or they are used in combination with halogen-containing cocatalysts. Halogen from such catalyst systems can be incorporated into the dimerization products, which considerably affects both the product quality and the further processing, in particular the hydroformylation to surfactant alcohols.
  • the heterogeneous catalyst can be used in a fixed bed - then preferably in coarse-grained form as 1 to 1.5 mm grit - or suspended (particle size 0.05 to 0.5 mm).
  • the dimerization is advantageously carried out at temperatures from 80 to 200 ° C., preferably from 100 to 180 ° C., below that at which
  • Reaction temperature prevailing pressure optionally also under a
  • reaction mixture is circulated several times, with a certain proportion of the circulating product being continuously discharged and replaced by starting material.
  • dimerization mixtures of monounsaturated hydrocarbons are obtained, the components of which predominantly have twice the chain length as the starting olefins.
  • the dimerization catalysts and the reaction conditions are expediently chosen within the scope of the above information so that at least 80% of the components of the dimerization mixture are in the range from 1/4 to 3/4, preferably from 1/3 to 2/3, of the chain length of their main chain have one branch or two branches on adjacent carbon atoms.
  • Very characteristic of the olefin mixtures produced according to the invention is their high proportion - generally over 75%, in particular over 80% - of components with branches and the low proportion - generally below 25, in particular below 20% - unbranched olefins.
  • Another characteristic is that predominantly groups with (y-4) and (y-5) carbon atoms are bound at the branching points of the main chain, where y is the number of carbon atoms of the monomer used for the dimerization.
  • the value (y-5) 0 means that there is no side chain.
  • the main chain preferably carries methyl or ethyl groups at the branching points.
  • the proportions of mono-substitution products (single branching) in the olefin mixture prepared according to the invention are typically in the range from 40 to 75% by weight, the proportions of double-branched components in the range from 5 to 25% by weight.
  • the dimerization mixtures can be derivatized particularly well if the position of the double bond meets certain requirements.
  • olefinic hydrogen atoms are those that are attached to a carbon atom that has a pi bond with the neighboring one Carbon atom.
  • novel olefin mixtures obtainable by the process according to the invention with the above-mentioned stucco characteristics are also an object of the present invention. They represent valuable intermediates, in particular for the production of branched primary alcohols and surfactants described below, but can also be used as starting materials in other technical processes based on olefins, in particular if the end products are to have improved biodegradability.
  • the olefin mixtures according to the invention are to be used for the production of surfactants, they are first derivatized to surfactant alcohols by methods known per se.
  • olefins resulting from process step c) are expediently hydrated by direct water addition with proton catalysis.
  • direct water addition with proton catalysis.
  • This is also possible, for example, by adding high-proof sulfuric acid to an alkanol sulfate and subsequent saponification to the alkanol.
  • the more expedient direct addition of water is carried out in the presence of acidic, in particular heterogeneous, catalysts and generally with the highest possible olefin partial pressure and at the lowest possible temperatures.
  • phosphoric acid on supports such as SiO 2 or Celite
  • acidic ion exchangers have proven to be effective catalysts.
  • the choice of conditions depends on the reactivity of the olefins to be reacted and can be routinely determined by preliminary tests (Lit .: e.g. AJ.Kresge et al. J.Am.Chem.Soc. 93, 4907 (1971); Houben-Weyl Vol. 5/4 (1960), pages 102-132 and 535-539).
  • the hydration generally leads to mixtures of primary and secondary alkanols in which the secondary alkanols predominate.
  • Another preferred object of the present invention is therefore a process for the preparation of mixtures of primary alkanols, which inter alia. suitable for further processing into surfactants, by hydroformylation of olefins, which is characterized in that the olefin mixtures according to the invention described above are used as the starting material.
  • the molar ratio of n- and iso-compounds in the reaction mixture is generally in the range from 1: 1 to 20: 1, depending on the process conditions chosen for the hydroformylation and the catalyst used.
  • the hydroformylation is normally carried out in the temperature range from 90 to 200 ° and at a CO / H 2 pressure of 2.5 to 35 MPa (25 to 350 bar).
  • the mixing ratio of carbon monoxide to hydrogen depends on whether alkanals or alkanols should preferably be produced.
  • catalysts are metal compounds of the general formula HM (CO) 4 or M 2 (CO) 8 , where M is a metal atom, preferably a cobalt, rhodium or ruthenium atom.
  • catalytically active species of the general formula H x M y (CO) z L q are formed from the catalysts or catalyst precursors used in each case, where M is a metal from subgroup VIII, L is a ligand which is a phosphine or phosphite , Amine, pyridine or any other donor compound, also in polymeric form, and q, x, y and z are integers, depending on the valency and type of the metal and the binding force of the ligand L, where q is also 0 can be.
  • the metal M is preferably cobalt, ruthenium, rhodium, palladium, platinum, osmium or iridium and in particular cobalt, rhodium or ruthenium.
  • Suitable rhodium compounds or complexes are, for example, rhodium (II) and rhodium (III) salts, such as rhodium (III) chloride, rhodium (III) nitrate, rhodium (III) sulfate, potassium rhodium sulfate, rhodium (II ) or rhodium (III) carboxylate, rhodium (II) and rhodium (III) acetate, rhodium (III) oxide, salts of rhodium (III) acid, such as trisammonium hexachlororhodate (III).
  • rhodium (II) and rhodium (III) salts such as rhodium (III) chloride, rhodium (III) nitrate, rhodium (III) sulfate, potassium rhodium sulfate, rh
  • Rhodium complexes such as rhodium biscarbonyl acetylacetonate, acetylacetonato bisethylene rhodium (I) are also suitable. Rhodium biscarbonyl acetylacetonate or rhodium acetate are preferably used.
  • Suitable cobalt compounds are, for example, cobalt (II) chloride, cobalt (II) sulfate, cobalt (II) carbonate, cobalt (II) nitrate, their amine or hydrate complexes, cobalt carbocylates such as cobalt acetate, cobalt ethyl hexanoate, cobalt naphthenoate, and the cobalt caprolactamate complex.
  • the carbonyl complexes of cobalt such as dicobalt octocarbonyl, tetrakobalt dodecacarbonyl and hexacobalt hexadecacarbonyl can be used.
  • the hydroformylation can be carried out with the addition of inert solvents or diluents or without such an addition.
  • Suitable inert additives are, for example, acetone, methyl ethyl ketone, cyclohexanone, toluene, xylene, chlorobenzene, methylene chloride, hexane, petroleum ether, acetonitrile and the high-boiling fractions from the hydroformylation of the dimerization products.
  • the hydroformylation product obtained has too high an aldehyde content, this can easily be achieved by hydrogenation, for example using hydrogen in the presence of Raney nickel or using other known hydrogenation reactions, in particular copper, zinc, cobalt, nickel, molybdenum, zirconium or Titanium-containing catalysts can be eliminated.
  • the aldehyde components are largely hydrogenated to alkanols.
  • a practically complete removal of aldehyde fractions in the reaction mixture can, if desired, be achieved by post-hydrogenation, for example under particularly gentle and economical conditions with an alkali metal borohydride.
  • the mixtures of branched primary alkanols which can be prepared by hydroformylation of the olefin mixtures according to the invention are likewise a subject of the present invention.
  • Non-ionic or anionic surfactants can be prepared from the alkanols according to the invention in different ways.
  • Nonionic surfactants are obtained by reacting the alkanols with alkylene oxides
  • R 1 is hydrogen or a straight-chain or branched aliphatic radical of the formula C n H 2n + 1 and n is a number from 1 to 16, preferably from 1 to 8.
  • R L is hydrogen, methyl or ethyl.
  • the alkanols of the invention can be reacted with a single alkylene oxide species or with several different ones.
  • compounds are formed which in turn carry an OH group and can therefore react again with an alkylene oxide molecule.
  • reaction products are therefore obtained which have more or less long polyether chains.
  • the polyether chains can contain 1 to about 200 alkylene oxide assemblies. Compounds whose polyether chains contain 1 to 10 alkylene oxide assemblies are preferred.
  • the chains can consist of the same chain links, or they can have different Akylenoxid construction groups, which differ from each other with respect to their rest R 1 . These different assemblies can exist within the chain in statistical distribution or in the form of blocks.
  • reaction scheme is intended to illustrate the alkoxylation of the alkanols according to the invention using the example of a reaction with two different alkylene oxides which are used in different molar amounts x and y.
  • R 1 and R la are different radicals within the scope of the definitions given above for R 1 and R 2 -OH is a branched alkanol according to the invention.
  • the alkoxylation is preferably catalyzed by strong bases which are advantageously added in the form of an alkali metal hydroxide or alkaline earth metal hydroxide, generally in an amount of 0.1 to 1% by weight, based on the amount of the alkanol R 2 -OH.
  • bases which are advantageously added in the form of an alkali metal hydroxide or alkaline earth metal hydroxide, generally in an amount of 0.1 to 1% by weight, based on the amount of the alkanol R 2 -OH.
  • Acid catalysis of the addition reaction is also possible.
  • Lewis acids such as A1C1 3 or BF 3 are also suitable. (See PHPlesch, The Chemistry of Cationic Polymerization, Pergamon Press, New York (1963)).
  • the addition reaction is carried out at temperatures from about 120 to about 220 ° C., preferably from 140 to 160 ° C., in a closed vessel.
  • the alkylene oxide or the mixture of different alkylene oxides is fed to the mixture of the alkanol mixture according to the invention and alkali under the vapor pressure of the alkylene oxide mixture prevailing at the selected reaction temperature.
  • the alkylene oxide can be diluted up to about 30 to 60% with an inert gas. This provides additional security against explosive polyaddition of the alkylene oxide.
  • polyether chains are formed in which the various alkylene oxide structures are virtually statistically distributed. Variations in the distribution of the building blocks along the polyether chain result from different reaction rates of the components and can also be achieved arbitrarily by continuously feeding an alkylene oxide mixture of program-controlled composition. If the various alkylene oxides are reacted in succession, polyether chains with block-like distribution of the alkylene oxide building blocks are obtained.
  • the length of the polyether chains fluctuates statistically around an average value within the reaction product, essentially the stoichiometric value resulting from the amount added.
  • alkoxylates which can be prepared starting from olefin mixtures and alkanol mixtures according to the invention likewise form a subject of the present invention They show a very good surface activity and can therefore be used as neutral surfactants in many areas of application.
  • surface-active glycosides and polyglycosides can also be prepared. These substances also have very good surfactant properties. They are obtained by one or more reactions (glycosidation or polyglycosidation) of the alkanol mixtures according to the invention with mono-, di- or polysaccharides with the exclusion of water with acid catalysis. Suitable acids are, for example, HC1 or H 2 SO 4 . As a rule, OUgoglycosides with statistical chain length distribution are obtained, the average degree of oligomerization being 1 to 3 saccharide residues.
  • the saccharide is first subjected to acid catalysis with a low molecular weight alkanol, e.g. Butanol, acetalized to butanol glycoside.
  • a low molecular weight alkanol e.g. Butanol
  • This reaction can also be carried out with aqueous solutions of the saccharide.
  • the lower alkanol glycoside for example the butanol glycoside, is then reacted with the alkanol mixtures according to the invention to give the desired glycosides according to the invention.
  • Excess long and short chain alkanols can be neutralized from the equilibrium mixture, e.g. by distillation in vacuo.
  • O-acetyl compounds of the saccharides are converted with hydrogen halide, which is preferably dissolved in glacial acetic acid, into the corresponding O-acetyl halosaccharides, which react with the alkanols to form the acetylated glycosides in the presence of acid-binding agents.
  • Monosaccharides are preferred for the glycosidation of the alkanol mixtures according to the invention, namely both hexoses such as glucose, fructose, galactose, mannose and pentoses such as arabinose, xylose or ribose.
  • Particularly preferred for Glycosidation of the alkanol mixtures according to the invention is glucose.
  • Mixtures of the saccharides mentioned can of course also be used for the glycosidation.
  • glycosides with statistically distributed sugar residues are then obtained.
  • the glycosidation can also be carried out several times, so that polyglycoside chains are added to the hydroxyl groups of the alkanols.
  • the saccharide building blocks can be randomly distributed within the chain or form blocks of the same structural groups.
  • furanose or pyranose structures can be obtained.
  • the reaction can also be carried out in suitable solvents or diluents.
  • glycosides and polyglycosides which can be prepared starting from olefin mixtures and alkanol mixtures according to the invention likewise constitute an object of the present invention.
  • Both the alkanol mixtures according to the invention and the polyethers prepared therefrom can be converted into anionic surfactants by esterifying (sulfated) them in a manner known per se with sulfuric acid or sulfuric acid derivatives to give acidic alkyl sulfates or alkyl ether sulfates or with phosphoric acid or its derivatives to give acidic alkyl phosphates or alkyl ether phosphates.
  • Sulfation reactions of alcohols have already been described, for example, in US Pat. Nos. 3,462,525, 3,420,875 or 3,524,864. Details of how this reaction is carried out can also be found in "Ullmanns Encyclopedia of Industrial Chemistry", 5th edition, volume A25 (1994 ), Pages 779-783 and in the literature references given there.
  • sulfuric acid itself is used for the esterification, it is expedient to use a 75 to 100% by weight, preferably 85 to 98% by weight acid (so-called “concentrated sulfuric acid” or “monohydrate”).
  • the esterification can be carried out in a solvent or diluent if it is necessary for the control of the reaction, e.g. the development of heat is desired.
  • the alcoholic reactant is initially introduced and the sulfating agent is added gradually with constant mixing. If complete esterification of the alcohol component is desired, the sulfating agent and the alkanol are used in a molar ratio of 1: 1 to 1: 1.5, preferably 1: 1 to 1: 1.2.
  • sulfating agent can be advantageous if mixtures of alkanol alkoxylates according to the invention are to be used and combinations of neutral and anionic surfactants are to be produced.
  • the esterification is normally carried out at temperatures from room temperature to 85 ° C., preferably in the range from 45 to 75 ° C.
  • sulfur trioxide sulfur trioxide complexes, solutions of sulfur trioxide in sulfuric acid ("oleum"), chlorosulfonic acid, sulfuryl chloride or also amidosulfonic acid can also be used to sulfate the alkanol mixtures according to the invention.
  • the reaction conditions must then be adjusted accordingly. If sulfur trioxide is used as the sulfating agent, the reaction can also advantageously be carried out in a falling film reactor in countercurrent, if desired also continuously.
  • the batches are neutralized by adding alkali and, if necessary, after removal of excess alkali sulfate and any solvents present, worked up.
  • the acidic alkanol sulfates and alkanol ether sulfates and their salts obtained by sulfating alkanols and alkanol ethers and their mixtures according to the invention are also a subject of the present invention.
  • alkanols and alkanol ethers according to the invention and their mixtures with phosphating agents can also be converted (phosphated) to acidic phosphoric acid esters.
  • Suitable phosphating agents are primarily phosphoric acid, polyphosphoric acid and phosphorus pentoxide, but also POCl 3 if the remaining acid chloride functions are subsequently hydrolysed.
  • the phosphating of alcohols has been described, for example, in Synthesis 1985, pages 449 to 488.
  • the acid alkanol phosphates and alkanol ether phosphates obtained by phosphating alkanols and alkanol ethers according to the invention and their mixtures are also a subject of the present invention.
  • alkanol ether mixtures alkanol glycosides which can be prepared starting from the olefin mixtures according to the invention, and the acidic ones PF 0000053264 / BM
  • 704 g 3 -hexene produced by metathesis of a C4 olefin stream ex FCC + catalytic distillation as in Example 6, are at a flow of 37 g / h at 60 ° C. in a tube reactor containing 793 g of a NiO / SiO2 / TiO2 Contains mixed catalyst.
  • the discharge is separated by distillation into C6 and high boilers (C12 +) by means of a packed column, unreacted hexene is returned to the reactor (102 g / h, conversion in a single pass approx. 27%).
  • the high boiler discharge is then separated into its components by distillation.
  • the dodecene isomer mixture obtained can be used in the hydroformylation (see Examples 13).
  • Example 13 Hydroformylation of the dodecene prepared by metathesis of various C4 olefin streams and dimerization of the hexene obtained therefrom
  • 2460 g of an oxo product produced in this way are hydrogenated in a 51-stroke stirred autoclave with the addition of 10% by weight of water with 100 g of Raney nickel at 150 ° C. and a hydrogen pressure of 280 bar for 15 hours.
  • the mixture is then allowed to come to room temperature, the pressure is released and the discharge is suctioned off through diatomaceous earth. After fractional distillation, 1947 g of a tridecanol mixture are obtained.
  • Example 14 Hydroformylation of the dodecene produced by metathesis of various C4 olefin streams and dimerization of the hexene obtained therefrom
  • Example 15 Hydroformylation of the dodecene produced by metathesis of various C4 olefin streams and dimerization of the hexene obtained therefrom
  • the dodecene was continuously hydroformylated in two cascaded stirred autoclaves, using 15 ppm of rhodium biscarbonyl acetylacetonate and 210 ppm of a polyethyleneimine in which 60% of all nitrogen atoms are acylated with lauric acid.
  • the reaction discharge was separated in a wiper blade evaporator at 170 ° C and 20 mbar.
  • the oxo products produced were subjected to fixed bed hydrogenation in a trickle mode, a Co / Mo fixed bed catalyst being used.
  • the reaction was carried out at 170 ° C. and 280 bar of hydrogen with the addition of 10% by weight of water under a load of 0.1 kg / 1 h. - 54 -
  • the OH number of the tridecanol shown is 278 mg KOH / g.

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  • 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)
  • Emulsifying, Dispersing, Foam-Producing Or Wetting Agents (AREA)

Abstract

L'invention concerne un procédé de production d'alcools tensioactifs et d'éthers d'alcools tensioactifs par dérivation d'oléfines ayant approximativement entre 10 à 20 atomes de carbone ou par dérivation de mélanges de telles oléfines et éventuellement par alcoxylation consécutive. Le procédé consiste à a) soumettre à une métathèse un mélange d'oléfines C4 avec un rapport 1-butène/2-butène = 1,2, b) à isoler les oléfines ayant 5 à 8 atomes de carbone du mélange métathèse, c) à soumettre à une dimérisation les oléfines isolées individuellement ou en mélange pour obtenir des mélanges d'oléfines ayant 10 à 16 atomes de carbone, d) après un éventuel fractionnement, à soumettre le mélange d'oléfines ainsi obtenu à une dérivatisation pour obtenir un mélange d'alcools tensioactifs et e) éventuellement à alcoxyler les alcools tensioactifs. Le mélange d'oléfines obtenu lors de la dimérisation a une fraction élevée de composantes ramifiées et moins de 10 % en poids de composés contenant un groupe vinylidène. L'invention concerne également l'utilisation d'alcools tensioactifs et d'éthers d'alcools tensioactifs pour produire des tensioactifs par glycosylation ou polyglycosylation, sulfatation ou phosphatation.
EP03706531A 2002-02-19 2003-02-19 Procede modifie de production d'alcools tensioactifs et d'ethers d'alcools tensioactifs, produits ainsi obtenus et leur utilisation Withdrawn EP1478609A2 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE10206845A DE10206845A1 (de) 2002-02-19 2002-02-19 Modifiziertes Verfahren zur Herstellung von Tensidalkoholen und Tensidalkoholethern, die hergestellten Produkte und ihre Verwendung
DE10206845 2002-02-19
PCT/EP2003/001668 WO2003070669A2 (fr) 2002-02-19 2003-02-19 Procede modifie de production d'alcools tensioactifs et d'ethers d'alcools tensioactifs, produits ainsi obtenus et leur utilisation

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EP1478609A2 true EP1478609A2 (fr) 2004-11-24

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US (1) US20050107628A1 (fr)
EP (1) EP1478609A2 (fr)
JP (1) JP2005517728A (fr)
KR (1) KR20040091634A (fr)
CN (1) CN1635984A (fr)
AU (1) AU2003208874A1 (fr)
DE (1) DE10206845A1 (fr)
WO (1) WO2003070669A2 (fr)

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EP3658651B1 (fr) * 2017-07-27 2025-06-18 SABIC Global Technologies B.V. Procédé de production d'un additif de carburant
SG11202008334VA (en) 2018-03-19 2020-09-29 Sabic Global Technologies Bv Method of producing a fuel additive
CN112135809A (zh) 2018-05-18 2020-12-25 沙特基础工业全球技术有限公司 利用水合单元生产燃料添加剂的方法
CN113544238B (zh) 2019-03-08 2023-02-28 沙特基础工业全球技术有限公司 生产燃料添加剂的方法
CN115515919A (zh) * 2020-05-29 2022-12-23 陶氏环球技术有限责任公司 具有混合的c8-c18醇的组合物及其表面活性剂
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JP2005517728A (ja) 2005-06-16
WO2003070669A2 (fr) 2003-08-28
US20050107628A1 (en) 2005-05-19
KR20040091634A (ko) 2004-10-28
DE10206845A1 (de) 2003-08-28
AU2003208874A1 (en) 2003-09-09
CN1635984A (zh) 2005-07-06
WO2003070669A3 (fr) 2004-02-05

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