EP1343742A1 - Method for the production of alkyl aryl sulphonates - Google Patents

Abstract

The production of alkyl aryl compounds can be achieved by the following steps: 1) production of an olefin mixture, comprising, as a statistical mean, predominantly single-branched C>10-14< olefins, by means of a) reaction of a C>4< olefin mixture on a metathesis catalyst to give an olefin mixture containing 2-pentene and/or 3-hexene and optional separation of 2-pentene and/or 3-hexene, followed by dimerisation of the obtained 2-pentene and/or 3-hexene on a dimerisation catalyst to give a mixture containing C>10-12< olefins and optional separation of the C>10-12< olefins, or b) extraction of predominantly single-branched paraffins from kerosene fractions and subsequent dehydrogenation, or c) Fischer-Tropsch synthesis of olefins or paraffins, whereby the paraffins are dehydrogenated, or d) dimerisation of short-chain internal olefins, or e) isomerisation of linear olefins or paraffins, whereby the isomerised paraffins are dehydrogenated, 2) reaction of the olefin mixture obtained in step 1) with an aromatic hydrocarbon in the presence of an alkylation catalyst containing zeolites of the faujasite type.

Description

 Process for the preparation of alkylarylsulfonates

The present invention relates to processes for the preparation of alkylaryl compounds and alkylarylsulfonates, alkylaryls and alkylarylsulfonates obtainable by these processes, the use of the latter as surfactants, preferably in detergents and cleaning agents, and detergents and cleaning agents containing them.

Alkylbenzenesulfonates (ABS) have long been used as surfactants in detergents and cleaning agents. After such surfactants based on tetrapropylene benzene sulfonate were initially used, but which were poorly biodegradable, linear benzene sulfonates (LAS) which were as linear as possible were subsequently produced and used. However, linear alkylbenzenesulfonates do not have adequate property profiles in all areas of application.

For example, it would be beneficial to improve their cold wash properties or their properties in hard water. The ease of formulation, given the viscosity of the sulfonates and their solubility, is also desirable. These improved properties show slightly branched compounds or mixtures of slightly branched compounds with linear compounds, but the right amount of branching and / or the right amount of mixture must be achieved. Branches that are too strong adversely affect the biodegradability of the products. Products that are too linear adversely affect the viscosity and solubility of the sulfonates.

In addition, the ratio of terminal phenylalkanes (2-phenylalkanes and 3-phenylalkanes) to internal phenylalkanes (4-, 5-, 6- etc. phenylalkanes) plays a role in the product properties. A 2-phenyl content of approximately 20-40% and a 2- and 3-phenyl content of approximately 40-60% can be advantageous in terms of product quality (solubility, viscosity, washing properties, biodegradability). Surfactants with very high 2- and 3-phenyl contents can have the major disadvantage that the processability of the products suffers from a sharp increase in the viscosity of the sulfonates.

In addition, a non-optimal solubility behavior can result. For example, the Krafft point of a solution of LAS with very high or very low 2- and 3-phenyl levels up to 10-20 ° C higher than with the optimal choice of the 2- and 3-phenyl levels.

BR 9204326 relates to the alkylation of aromatics with linear olefins on modified Fauj asit zeolites.

EP-A-0 160144 describes the alkylation of aromatics with predominantly long-chain olefins (for example Cι ₆ ) over partially collapsed FAU structures.

No. 5,030,786 describes the drying of an aromatic and olefinic feedstock and the subsequent alkylation over FAU or BEA zeolites. Ethene and propene are preferably used as olefinic feedstocks.

US 4,990,718 describes the oligomerization of di- or C ₆ alpha-.ι 01efinen and the subsequent alkylation of aromatic hydrocarbons. with the dimerization products, which have a branching ratio of 0.1-0.19, on zeolites with a pore size of 6.4-7.5 Å, predominantly zeolites of the faujasite type.

WO 99/05241 relates to cleaning agents which contain branched alkylarylsulfonates as surfactants. The alkylarylsulfonates are obtained by dimerization of olefins to vinylidene olefins and subsequent alkylation of benzene over a shape-selective catalyst such as MOR or BEA. This is followed by sulfonation.

WO 90/14160 describes special zeolites of the faujasite type for alkylation. Ethylbenzene and cumene are produced using these catalysts.

The olefins hitherto used for alkylation either have no branches at all, which contradicts the concept of the present invention, or in some cases show too high or too low a degree of branching or result in a non-optimal ratio of termial to internal phenylalkanes. On the other hand, they are made from expensive raw materials such as propene or alpha-olefins, and in some cases the proportion of olefin reactions of interest for the preparation of surfactants is only about 20%. This leads to expensive refurbishment steps. In addition, catalysts are used whose low space / time yields, high deactivation rates and high catalyst costs prevent the processes from being carried out economically.

The object of the present invention is to provide a process for the preparation of alkylarylsulfonates or the underlying alkylaryl compounds which are at least partially branched and thus have advantageous properties over the known compounds for use in detergents and cleaning agents. In particular, they should have a suitable property profile from biodegradability, insensitivity to water hardness, solubility and viscosity during production and use. In addition, the alkylarylsulfonates should be inexpensive to produce.

The object is achieved according to the invention by a process for the preparation of alkylaryl compounds

1) Production of a mixture of Cio-π-olefins, predominantly single-branched on average, by

a) reaction of a C ₄ -olefin mixture over a methathesis catalyst to produce an olefin mixture containing 2-pentene and / or 3-hexene and, if appropriate, separation of 2-pentene and / or 3-hexene, followed by dimerization of the 2- Pentens and or 3-

Hexens on a dimerization to a mixture containing C ₁₀ -ι ₂ -olefins and optionally separating the C ₁₀ -ι ₂ -olefins, or

b) extraction of predominantly single-branched paraffins from kerosene cuts and subsequent dehydration, or

c) Fischer-Tropsch synthesis of olefins or paraffins, the paraffins being dehydrated, or

d) dimerization of short-chain internal olefins, or e) isomerization of linear olefins or paraffins, the isomerized paraffins being dehydrated,

2) Reaction of the olefin mixture obtained in stage 1) with an aromatic hydrocarbon in the presence of an alkylation catalyst which contains faujasite-type zeolites.

The alkylaryl compounds obtained are subsequently sulfonated and neutralized in stage 3).

The combination of zeolite faujasite as the alkylation catalyst with the olefins obtained from stages la) to le) gives products which, after sulfonation and neutralization, give surfactants which have outstanding properties, in particular with regard to sensitivity to hardness-forming ions and the solubility of the sulfonates , the viscosity of the sulfonates and their washing properties. In addition, the present process is extremely inexpensive, since the product streams can be designed so flexibly that no by-products are produced.

Starting from a C ₄ stream, linear internal olefins are produced in stage la) by the metathesis, which are then converted into branched olefins via the dimerization step.

The process according to the invention with stage la offers the significant advantage that the combination of metathesis and dimerization results in an olefin mixture which, after alkylation of an aromatic with the catalysts according to the invention, sulfonation and neutralization, provides a surfactant which is characterized by its combination of excellent application properties ( Solubility, viscosity, stability against water hardness, washing properties, biodegradability). With regard to the biodegradability of alkylarylsulfonates, compounds which are less strongly adsorbed on sewage sludge or which have a higher bioavailability than conventional LAS due to reduced precipitation due to water hardness are particularly advantageous.

According to the invention, the process for the preparation of alkylarylsulfonates can have the following features: Preparation of a mixture of slightly branched olefins with a total C number of 10-14.

Reaction of the olefin mixture obtained in stage 1) with an aromatic hydrocarbon in the presence of an alkylation catalyst of the faujasite type to form alkylaromatic compounds, it being possible for additional linear olefins to be mixed in before the reaction.

Sulfonation and neutralization of the alkyl aromatic compounds obtained in stage 2) and neutralization to alkylarylsulfonates, where before

Sulfonation linear alkylbenzenes can also be added.

Possibly. Mix the alkylarylsulfonates obtained in stage 2) with linear alkylarylsulfonates.

Stage 1) of the process according to the invention is the preparation of a mixture of slightly branched olefins with a total C number of 10-14.

la)

The reaction of a C -olefin mixture over a metathesis catalyst is preferred for the production of an olefin mixture containing 2-pentene and / or 3-hexene and optionally separation of 2-pentene and / or 3-hexene. The metathesis can be carried out, for example, as described in DE-A-199 32 060. The 2-pentene and / or 3-hexene obtained is dimerized on a dimerization catalyst to give a C ₁₀ -ι ₂ - olefin mixture. If necessary, the Cιo -01-refines obtained are separated off.

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 the VI.b, VI.b or VM. Group of the Periodic Table of the Elements applied to inorganic supports.

Is preferred as metathesis catalyst is rhenium oxide on a support, preferably used in γ-aluminum oxide or on Al2θ ₃ / B ₂ O ₃ / Si0 ₂ -Mischträgern. In particular, the catalyst used is Re ₂ O ₇ / γ-Al ₂ O ₃ with a rhenium oxide content of 1 to 20% by weight, preferably 3 to 15% by weight, particularly preferably 6 to 12% by weight.

In the liquid mode of operation, the metathesis is preferably carried out at a temperature of 0 to 150 ° C., particularly preferably 20-80 ° C. and a pressure of 2-200 bar, particularly preferably 5-30 bar.

If the metathesis is carried out in the gas phase, the temperature is preferably 20 to 300 ° C., particularly preferably 50 to 200 ° C. In this case, the pressure is preferably 1 to 20 bar, particularly preferably 1 to 5 bar.

The production of Cs / Co-olefins and, if appropriate, propene from steam cracker or refinery C streams can comprise the substeps (1) to (4):

(1) Separation of butadiene and acetylenic compounds by optionally extracting butadiene with a butadiene-selective solvent and subsequently / or selectively hydrogenating butadienes and acetylenic impurities contained in crude C ₄ cuts in order to obtain a reaction product, the n-butenes and isobutene and contains essentially no butadienes and acetylenic compounds,

(2) Separation of isobutene by reacting the reaction discharge obtained in the above step with an alcohol in the presence of an acid catalyst to give an ether, separation of the ether and the alcohol, which can be carried out simultaneously or after etherification, to obtain a reaction discharge which Contains n-butenes and, if appropriate, oxygenate impurities, where ether formed can be discharged or cleaved back to obtain pure isobutene and the etherification step can be followed by a distillation step to separate isobutene, C ₃ -, iC ₄ - and Cs hydrocarbons optionally also being introduced by distillation can be separated in the course of working up the ether, or oligomerization or polymerization of isobutene from the reaction product obtained in the above step in the presence of an acid catalyst, the acid strength of which is suitable for the selective removal of isobutene as oligo- or polyisobutene to obtain a stream which has 0 to 15% residual isobutene, (3) separating the oxygenate impurities from the discharge of the above steps on appropriately selected absorber materials,

(4) Metathesis reaction of the raffinate II stream thus obtained as described.

The sub-step selective hydrogenation of butadiene and acetylenic impurities contained in crude C _{4 cut} is preferably carried out in two stages by contacting the raw C cut in the liquid phase with a catalyst which comprises at least one metal selected from the group consisting of nickel, palladium and platinum. contains on a carrier, preferably palladium on aluminum oxide, at a temperature of 20 to 200 ° C, a pressure of 1 to 50 bar, a volume velocity of 0.5 to 30 m ³ fresh feed per m ³ catalyst per hour and a ratio of recycle to feed from 0 to 30 with a molar ratio of hydrogen to diolefins from 0.5 to 50 in order to obtain a reaction product in which, in addition to isobutene, the n-butenes 1-butene and 2-butene in a molar ratio of 2: 1 to 1 : 10, preferably from 2: 1 to 1: 3, and essentially no diolefins and acetylenic compounds are present. For a maximum hexene discharge, 1-butene is preferably present in excess, for a high propene yield, 2-butene is preferably present in excess. This means that the total molar ratio in the first case can be 2: 1 to 1: 1 and in the second case 1: 1 to 1: 3.

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, after the subsequent selective hydrogenation / isomerization, 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: 3.

The sub-step 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 is 0.8 to 2.0, preferably 1.0 to 1.5 and the total conversion corresponds to the equilibrium conversion.

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 or Lewis Acids, see DE-A-100 13 253.

The dimerization of the olefins or olefin mixtures obtained in the metathesis step gives dimerization products which have particularly favorable components and particularly advantageous compositions with regard to the further processing to give alkylaromatics.

For a more detailed description of the metathesis / dimerization process and the upstream steps, reference is made to DE-A-199 32 060.

In addition to the metathesis / dimerization reaction just described, however, conventional processes for producing slightly branched olefins can also be carried out. This is e.g. lb) the extraction of i-paraffins from diesel / kerosene fractions, which either arise during crude oil processing and refinement or lc) are formed by synthetic processes such as Fischer-Tropsch synthesis, and optionally subsequent dehydrogenation of the i-paraffins i-olefins.

In addition, slightly branched olefins e.g. ld) are produced by the dimerization of shorter-chain olefins.

Another possibility is, for example, le) isomerization of suitable linear olefins to slightly branched olefins.

Step 2) is the reaction of the olefin mixture obtained in step 1) with an aromatic hydrocarbon in the presence of an alkylation catalyst of the faujasite type to form alkylaromatic compounds, it being possible for additional linear olefins to be mixed in before the reaction. An alkylation catalyst which leads to alkylaromatic compounds which have one to three carbon atoms in the alkyl radical with an H / C index of 1 is preferably used, or the reaction conditions are chosen accordingly.

When selecting the faujazite catalyst used according to the invention, regardless of the great influence of the feedstock used on the minimization of compounds formed by the catalyst, which are characterized in that they contain carbon atoms with an H / C index of 0 in the side chain to pay attention to. The proportion of carbon atoms in the alkyl radical with an HC index of 0 should, on average, be less than 5% (preferably less than 1%) of all compounds.

The H / C index defines the number of protons per carbon atom.

The olefins used in the process according to the invention preferably have no carbon atoms with an H / C index of 0 in the side chain. If the alkylation of the aromatic with the olefin is now carried out under conditions as described here and under which no skeletal isomerization of the olefin takes place, carbon atoms with an H C index of 0 can only be formed in the benzyl position to the aromatic, i.e. it is sufficient to determine the H / C index of the benzylic carbon atoms.

Furthermore, compounds are to be formed which have an average of 1 to 3 carbon atoms with an H / C index of 1 in the side chain. This is achieved in particular by selecting a suitable feedstock and suitable catalysts which, on the one hand, suppress the formation of the undesired products due to their geometry and, on the other hand, allow a sufficient reaction rate.

Catalysts for the process according to the invention are faujasite type zeolites, in particular zeolite Y and its derivatives. By descendants we mean modified faujasites, e.g. by processes such as ion exchange, steaming, blocking external centers, etc. The catalysts are distinguished in particular by the fact that they contain over 20% of a phase in the X-ray powder diffractogram which can be indexed with the cubic structure of the faujasite.

Although in the published literature (e.g. Cao et al, Appl. Cat. 184 (1999) 231; Sivasanker et al., J. Cat. 138 (1992) 386; Liang et al., Zeolites 17 (1996) 297; Almeida et al., Appl. Catal. 114 (1994) 141) that zeolites of the type faujasite (FAU) in In contrast to the zeolites mordenite (MOR) and beta (BEA) have practically no shape selectivity in the alkylation of aromatics with linear olefins - a similar approach can be found, for example, in WO 99/05082, where MOR and BEA zeolites for the reaction with branched olefins - it has now surprisingly been found that zeolites of the faujasite type exhibit shape-selective behavior in the alkylation of aromatic hydrocarbons (preferably benzene) with slightly branched olefins (preferably those from a metathesis / dimerization stage la) and, moreover, an optimal proportion of 2- and 3 -phenylalkanes produce with low catalyst costs - so HY is currently 3-4 times cheaper than H-MOR or H-BEA, have economically interesting space / time yields and moderate deactivation behavior.

Shape selectivity in heterogeneous catalysis describes the phenomenon of precursors, transition states, or products being excluded from participation in the reaction by a steric hindrance specified by the catalyst or not being allowed in the reaction. This phenomenon is of crucial importance with regard to the alkylbenzenes and alkylbenzenesulfonates according to the invention, in particular with regard to their H / C indices. While products are obtained with non-shape-selective catalysts which contain C atoms with H / C indices of 0 in the side chain, these compounds are excluded according to the invention with shape-selective catalysts.

However, catalysts with narrow pore systems always have the disadvantage that the space / time yields which can be achieved are lower than with catalysts with larger pores or with macro- or mesoporous substances. It is therefore important to find a catalyst which both fulfills the precondition of the desired shape selectivity, but additionally has the highest possible space / time yields, so that nothing stands in the way of the process being carried out economically.

In addition, it is known that pore systems that are too narrow are subject to strong and rapid deactivation, which likewise impairs the economics of the processes due to the need to regenerate the catalysts frequently.

When choosing the catalysts should also be based on their inclination with regard to

Deactivation must be respected. One-dimensional pore systems mostly have the disadvantage of rapid clogging of the pores by degradation or build-up products from the

Process on. In addition, the diffusion inhibition of the reactants and the products is in one-dimensional pore systems larger than in multi-dimensional. Catalysts with multidimensional pore systems are therefore preferred.

The catalysts used can be of natural or synthetic origin, the properties of which can be determined by methods known from the literature, such as e.g. in J. Weitkamp and L. Puppe, Catalysis and Zeolites, Fundamentals and Applications, Chapter 3: G. Kühl, Modification of Zeolites, Springer Verlag, Berlin, 1999 (ion exchange, dealumination, dehydroxylation and extraction of lattice aluminum, thermal treatment, steaming, Treatment with acids or SiCl, blocking of special, for example external, acidic centers by, for example, silylation, reinsertion of aluminum, treatment with aluminum halides and oxo acids) can be adjusted to a certain extent. It is important for the present invention that the catalysts have more than 10 μmol / g acid centers with a pKa value less than 3.3. The number of acidic centers is determined using the Hammett titration method with dimethyl yellow [CAS-No. 60-11-7] as an indicator and n-butylamine as a probe according to H.A. Benesi and B.H.C. Winquist in Adv. Catal., Vol. 27, Academic Press 1978, pp. 100 ff.

Furthermore, the catalysts may also contain used catalyst material or consist of such material which has been regenerated by the usual methods, e.g. B. by recalcination in air, H ₂ O, CO ₂ or inert gas at temperatures greater than 200 ° C, by washing with H ₂ O, acids or organic solvents, by steaming or by treatment in vacuo at temperatures greater than 200 ° C.

They can be used in the form of powder or, preferably, in the form of shaped articles such as strands, tablets or grit. Binder can be added for the shaping from 2 to 60% by weight (based on the mass to be shaped). Various aluminum oxides, preferably boehmite, amorphous aluminosilicates with a molar SiO ₂ / Al ₂ 0 ₃ ratio of 25:75 to 95: 5, silicon dioxide, preferably highly disperse Si0 ₂ such as silica sols, mixtures of highly disperse Si0 ₂ and highly disperse are suitable as binders A1 ₂ 0 ₃ , highly disperse TiO ₂ and clays.

After the shaping, the extrudates or compacts are expediently dried at 110 ° C./16 h and calcined at 300 to 500 ° C. for 2 to 16 h, the calcination optionally also being able to take place directly in the alkylation reactor. As a rule, the catalysts are used in the H form. To increase the selectivity, the service life and the number of possible catalyst regenerations, however, various modifications can also be made to the catalysts.

A modification of the catalysts is that the undeformed catalysts with alkali metals such as Na and K, alkaline earth metals such as Ca, Mg, earth metals such as TI, transition metals such as Mn, Fe, Mo, Cu, Zn, Cr, noble metals and / or rare earth metals such as eg Can exchange or dope La, Ce or Y ions.

An advantageous embodiment of the catalyst is that the deformed catalysts are placed in a flow tube and at 20 to 100 ° C z. B. a halide, an acetate, an oxalate, a citrate or a nitrate of the above-described metals in dissolved form. Such an ion exchange can e.g. B. on the hydrogen, ammonium and alkali form of the catalysts.

Another possibility of applying metal to the catalysts is that the zeolitic material z. B. impregnated with a halide, acetate, oxalate, citrate, nitrate or oxide of the above-described metals in aqueous or alcoholic solution.

Both ion exchange and impregnation can be followed by drying or, alternatively, repeated calcination. In the case of metal-doped catalysts, an aftertreatment with hydrogen and / or with water vapor can be advantageous.

Another possibility of modifying the catalyst is that the heterogeneous catalytic material - deformed or not deformed - is treated with acids such as hydrochloric acid (HC1), hydrofluoric acid (HF), phosphoric acid (H ₃ PO ₄ ), sulfuric acid (H ₂ SO) , Oxalic acid (HO ₂ C-CO ₂ H) or mixtures thereof.

A special embodiment consists in treating the catalyst powder with hydrofluoric acid (0.001 to 2 molar, preferably 0.05 to 0.5 molar) for 1 to 3 hours under reflux before it is deformed. After filtering off and washing out, it is generally dried at 100 to 160 ° C. and calcined at 400 to 550 ° C. Another special embodiment is an HCl treatment of the heterogeneous catalysts after they have been deformed with a binder. Here, the heterogeneous catalyst is usually treated for 1 to 3 hours at temperatures between 60 and 80 ° C with a 3 to 25%, in particular with a 12 to 20% hydrochloric acid, then washed out, dried at 100 to 160 ° C and at Calcined at 400 to 550 ° C.

Another possibility of modifying the catalyst is the exchange with ammonium salts, e.g. B. with NH4CI, or with mono-, di- or polyamines. Here, the heterogeneous catalyst deformed with the binder is generally continuously exchanged at 60 to 80 ° C. with 10 to 25%, preferably about 20%, NE ^ Cl solution for 2 hours in a 1:15 by weight heterogeneous catalyst / ammonium chloride solution and then dried at 100 to 120 ° C.

Another modification that can be made to aluminum-containing catalysts is dealuminization, in which some of the aluminum atoms are replaced by silicon or the aluminum content of the catalysts is reduced by, for example, hydrothermal treatment. A hydrothermal dealumination advantageously is followed by extraction with acids or complexing agents in order to remove non-lattice aluminum formed. Aluminum can be replaced by silicon, for example, using (NEW) ₂ SiF ₆ or SiCl ₄ . Examples of dealuminations of Y zeolites can be found in Corma et al., Stud. Surf. Be. Catal. 37 (1987), pages 495 to 503.

The modification by silylation is generally described in J. Weitkamp and L. Puppe, Catalysis and Zeolites, Fundamentals and Applications, Chapter 3: G. Kühl, Modification of Zeolites, Springer Verlag, Berlin, 1999. As a rule, the procedure is to selectively block acidic centers, for example the external ones, by means of donor bases such as, for example, 2,2,6,6, - tetramethylpiperidine or 2,6-lutidine, and then using suitable si- Compounds such as tetraethyl orthosilicate, tetramethyl orthosilicate, C1-C20 trialkylsilyl chloride, methylate or ethylate or SiCl treated. This treatment can take place both with gaseous Si compounds and with Si compounds dissolved in anhydrous solvents such as hydrocarbons or alcohols. A combination of different Si compounds is also possible. Alternatively, the Si compound can already contain the amine group which is selective for acidic centers, such as 2,6-trimethylsilylpiperidine. Subsequently, the catalysts modified in this way are generally calcined at from 200 to 500 ° C. in an atmosphere containing 0 ₂ . Another modification consists in blocking external centers by mixing or grinding the catalyst powder with metal oxides such as MgO and subsequent calcining at 200-500 ° C.

The catalysts can be used as strands with diameters of z. B. 1 to 4 mm or as tablets with z. B. Use 3 to 5 mm diameter for aromatic alkylation.

The type of aliphatic raw material used according to the invention and the choice of catalyst according to the invention lead to the optimal ratios of 2-, 3-, 4-, 5- and 6-phenylalkanes for detergent and cleaning agent applications. A 2-phenyl fraction of 20-40% and a 2- and 3-phenyl fraction of 40-60% are preferably produced.

Preferred reaction procedure

The alkylation is carried out in such a way that the aromatics (the aromatic mixture) and the olefin (mixture) are allowed to react in a suitable reaction zone by contacting the catalyst, the reaction mixture is worked up after the reaction and the valuable products are thus obtained.

Suitable reaction zones are e.g. Tubular reactors, stirred tanks or a stirred tank cascade, a fluidized bed, a loop reactor or a solid-liquid fluidized bed. If the catalyst is in solid form, it can be used either as a slurry, as a fixed bed, as a fluidized bed or as a fluidized bed.

When using a fixed bed reactor, the reactants can be run either in cocurrent or in countercurrent. Execution as a catalytic distillation is also possible.

The reactants are either in the liquid and / or in the gaseous state, but preferably in the liquid state. Reaction in the supercritical state is also possible.

The reaction temperature is chosen so that conversion of the olefin takes place as completely as possible on the one hand and as little by-products as possible on the other hand arise. By-products are primarily dialkylbenzenes, diphenylalkanes and olefin oligomers. The choice of temperature control also depends crucially on the catalyst chosen. Reaction temperatures between 50 ° C and 500 ° C (preferably 80 to 350 ° C, particularly preferably 80-250 ° C) can be used.

The pressure of the reaction depends on the chosen procedure (reactor type) and is between 0.1 and 100 bar, the catalyst load (WHSV) is selected between 0.1 and 100.

The reactants can optionally be diluted with inert substances. Inert substances are preferred paraffins.

The molar ratio of aroma olefin is usually set between 1: 1 and 100: 1 (preferably 2: 1-20: 1).

The process can be carried out discontinuously, semi-continuously by submitting e.g. Catalyst and aromatics and metering of olefin or fully continuously, optionally also with continuous feeding and removal of catalyst.

Catalyst with insufficient activity can pass directly in the alkylation reactor or in a separate plant

1) Washing with solvents such as Alkanes, aromatics such as Benzene, toluene or xylene, ethers such as e.g. Tetrahydrofuran, tetrahydropyran, dioxane, dioxolane, diethyl ether or methyl t-butyl ether, alcohols such as e.g. Methanol, ethanol, propanol and isopropanol, amides such as e.g. Dimethylformamide or formamide, nitriles such as e.g. Acrylonitrile or water at temperatures from 20 to 200 ° C,

2) by treatment with steam at temperatures from 100 ° C to 400 ° C

3) by thermal treatment in a reactive gas atmosphere (O ₂ and O ₂ -containing gas mixtures, C0 ₂ , CO, H ₂ ) at 200 - 600 ° C or

4) can be regenerated at 200 - 600 ° C by thermal treatment in an inert gas atmosphere (N ₂ , noble gases). Alternatively, as described above, deactivated catalyst can also be added during the production of new catalyst. Aromatic ingredients

All aromatic hydrocarbons of the formula Ar-R are possible, where Ar is a monocyclic or bicyclic aromatic hydrocarbon radical and R is selected from H, C, preferably C ₃ -C ₃ -alkyl, OH, OR, etc., preferably H or CM-alkyl. Benzene and toluene are preferred.

Level 3)

In stage 3), the alkyl aromatic compounds obtained in stage 2) are sulfonated and neutralized to alkylarylsulfonates. Alkylaryls are made by

Sulfonation (for example with SO ₃ , oleum, chlorosulfonic acid, etc., preferably with SO ₃ ) and subsequent ones

Neutralization (e.g. with Na, K, NHU, Mg compounds, preferably with Na compounds)

converted to alkylarylsulfonates. Sulfonation and neutralization are adequately described in the literature and are carried out according to the prior art. The sulfonation is preferably carried out in a falling film reactor, but can also be carried out in a stirred tank. The sulfonation with SO ₃ is preferable to the sulfonation with oleum.

mixtures

The compounds prepared by the processes described above are (preferably) either processed further as such, or previously mixed with other alkylarylene and then sent for further processing. In order to simplify this process, it can also make sense to mix the raw materials used for the production of the other alkylaryls mentioned above directly with the raw materials of the present process and then to carry out the process according to the invention. For example, the mixing of slightly branched olefin streams from the process according to the invention with linear olefins is useful. Mixtures of alkylarylsulfonic acids or alkylarylsulfonates can also be used. The mixtures are always made with a view to optimizing the product quality of the surfactants made from the alkylaryl. An exemplary overview of alkylation, sulfonation, neutralization is given, for example, by "Alkylarylsulfonates: History, Manufacture, Analysis and Environmental Properties" in Surf. Se. Ser. 56 (1996) Chapter 2, Marcel Dekker, New York and references contained therein.

Analysis of structural parameters

The alkylation of aromatics with olefins produces alkyl aromatics of the formulas R '"ArCH ₂ R (1), R'" ArCHRR '(2) and R'"ArCRR'R" (3). R '"denotes H or Q- C ₃ alkyl. The proportions of (1) - (3) are determined as shown below using the example of benzene as an aromatic:

1) The reactor discharge is distilled and unreacted aromatic, unreacted olefin and heavy alkylate, which is formed by alkylating the aromatic with more than one molecule of olefin, is separated off.

2) The proportion of (1) is then determined as follows:

25 mg of alkylbenzene and 5 mg of chromium acetylacetonate (CAS 21679-31-2) are dissolved in 500 mg of CDC1 ₃ and placed in an NMR sample tube with an inner diameter of 5 mm. A C13-NMR spectrum with a measuring frequency of 125 MHz is then recorded with an inverted-gated pulse sequence every 6 s and 6000 of these spectra are averaged. The sum spectrum is then standardized to CDC1 ₃ = 77.47 ppm. The proportion of structures of type (1) now results from

Proportion of (1) = (integral from 139 to 143.5 ppm) / (integral from 139 to 152 ppm)

3) Then the proportion of (2) is determined as follows:

5 mg of alkylbenzene and 0.5 mg of SiMe are dissolved in 500 mg of CDCI ₃ and placed in an NMR sample tube with an inner diameter of 5 mm. Then, with a 30 ° pulse sequence, an HI NMR spectrum with a 500 MHz measurement frequency is recorded every 5 s and 32 of these spectra are averaged. The sum spectrum is then normalized to SiMe ₄ = 0 ppm. The proportion of structures of type (2) now results from

Share of (2) = 5 * (integral from 2.2 to 3.2 ppm) / (integral from 6.9 to 7.6 ppm) - 2 * share of (l)

3) The proportion of (3) now results from the standardization condition Share in (1) + share in (2) + share in (3) = 100%

Aromatics other than benzene are determined analogously.

The invention also relates to alkylaryl compounds and alkylarylsulfonates which can be obtained by a process as described above.

The alkylarylsulfonates according to the invention are preferably used as surfactants, in particular in detergents and cleaning agents. The invention also relates to detergents and cleaning agents containing alkylarylsulfonates, as described above, in addition to conventional ingredients.

Non-exclusive examples of common ingredients of the washing and cleaning agents according to the invention are listed below:

bleach

Examples are alkali perborates or alkali carbonate perhydrates, especially the sodium salts.

An example of a usable organic peracid is peracetic acid, which is preferably used in commercial textile washing or cleaning. Bleaching agents or textile detergent compositions which can be used advantageously contain C 1 -C -percarboxylic acids, Cs - 1 - dipercarboxylic acids, imidopercaproic acids, or aryldipercarpronic acids. Preferred examples of usable acids are peracetic acid, linear or branched octanoic, nonanoic, decanoic or dodecane monoperacids, decanoic and dodecanediperic acid, mono- and diperphthalic acids, isophthalic acids and terephthalic acids, phthalimidopercaproic acid and terephthaloyldipercaproic acid. Polymeric peracids can also be used, for example those which contain basic acrylic acid units in which a peroxy function is present. The percarboxylic acids can be used as free acids or as salts of the acids, preferably alkali or alkaline earth metal salts.

bleach

Bleaching catalysts are, for example, quaternized imines and sulfonimines, as are described, for example, in US Pat. No. 5,360,568, US Pat. No. 5,360,569 and EP-A-0 453 003 also manganese complexes, as described, for example, in WO-A 94/21777. Further metal-containing bleaching catalysts which can be used are described in EP-A-0 458 397, EP-A-0 458 398, EP-A-0 549 272.

Bleach activators are, for example, compounds of the following substance classes: polyacylated sugars or sugar derivatives with C 1-20 acyl radicals, preferably acetyl, propionyl, octanoyl, nonanoyl or benzoyl radicals, particularly preferably acetyl radicals, can be used as bleach activators. Mono- or disaccharides and their reduced or oxidized derivatives can be used as sugar or sugar derivatives, preferably glucose, mannose, fructose, sucrose, xylose or lactose. Particularly suitable bleach activators of this class of substances are, for example, pentaacetylglucose, xylose tetraacetate, l-benzoyl-2,3,4,6-tetraacetylglucose and l-octanoyl-2,3,4,6-tetraacetylglucose.

Another class of substances that can be used are the acyloxybenzenesulfonic acids and their alkali metal and alkaline earth metal salts, it being possible to use Ci-π-acyl radicals. Acetyl, propionyl, octanoyl, nonanoyl and benzoyl residues are preferred, in particular acetyl residues and nonanoyl residues. Particularly suitable bleach activators in this class of substances are acetyloxybenzenesulfonic acid. They are preferably used in the form of their sodium salts.

O-Acyloxime esters such as. B. O-acetylacetone oxime, O-benzoylacetone oxime, bis (propylimino) carbonate, bis (cyclohexylimino) carbonate.

Acylated oximes which can be used according to the invention are described, for example, in EP-A-0 028 432. Oxime esters which can be used according to the invention are described, for example, in EP-A-0 267 046.

N-Acylcarprolactams such as N-acetylcaprolactam, N-benzoylcaprolactam, N-octanoylcaprolactam, carbonyl biscaprolactam can also be used.

Are still usable

N-diacylated and N, N'-tetraacylated amines, e.g. B. N, N, N ', N'-tetraacetylmethylene diamine and ethylenediamine (TAED), N, N-diacetylaniline, N, N-diacetyl-p-toluidine or 1,3-diacylated hydantoins such as 1,3-diacetyl-5 , 5-dimethylhydantoin;

N-alkyl-N-sulfonyl-carbonamides, for example N-methyl-N-mesyl-acetamide or N-methyl-N-mesyl-benzamide; N-acylated cyclic hydrazides, acylated triazoles or urazoles, for example monoacetyl-maleic acid hydrazide;

O, N, N-trisubstituted hydroxylamines, e.g. O-benzoyl-N, N-succinyl hydroxylamine,

O-acetyl-N, N-succinyl-hydroxylamine or 0, N ₅ N-triacetylhydroxylamine; - N, N '~ diacyl-sulfurylamide, for example N, N'-dimethyl-N, N'-diacetyl-sulfiιrylamide or

N, N'-diethyl-N, N'-dipropionyl-sulfurylamide;

Triacylcyanurates, e.g. Triacetyl cyanurate or tribenzoyl cyanurate;

Carboxylic anhydrides, e.g. Benzoic anhydride, m-chlorobenzoic anhydride or phthalic anhydride; - 1,3-diacyl-4,5-diacyloxyimidazolines, e.g. l, 3-diacetyl-4,5-diacetoxy;

Tetraacetylglycoluril and tetrapropionylglycoluril; diacylated 2,5-diketopiperazines, e.g. l, 4-diacetyl-2,5-diketopiperazine;

Acylation products of propylene diurea and 2,2-dimethylpropylene diamine, e.g. tetraacetylpropylenediurea; α-acyloxy polyacyl malonamides, e.g. -Acetoxy-N, N'-diacetyl malonamide;

Diacyl-dioxohexahydro-l, 3,5-triazines, e.g. l, 5-diacetyl-2,4-dioxohexahydro-l, 3,5-triazine.

1-Alkyl- or l-aryl- (4H) -3, l-benzoxazin-4-ones can also be used, as described, for example, in EP-B1-0 332 294 and EP-B 0 502 013. In particular 2-phenyl- (4H) -3, l-benzoxazin-4-one and 2-methyl- (4H) - 3, 1-benzoxazin-4-one can be used.

Cationic nitriles as described, for example, in EP 303 520 and EP 458 391 AI can also be used. Examples of suitable cation nitriles are the methosulfates or tosylates of trimethylammonium acetonitrile, N, N-dimethyl-N-octylammonium acetonitrile, 2- (trimethylammonium) propionitrile, 2- (trimethylammonium) -2-methyl-propionitrile, N-methylpiperazinium-N , N'-diacetonitrile and N-methylmo_holinium acetronitrile.

Particularly suitable crystalline bleach activators are tetraacetylethylene diamine (TAED), NOBS, isoNOBS, carbonyl biscaprolactam, benzoyl caprolactam, bis (2-propylimino) carbonate, bis (cyclohexylimino) carbonate, O-benzoylacetone oxime and 1-phenyl- (4H) -3, l-benzoxazine 4-one, anthranil, phenylanthranil, N-methylmorpholinoacetonitrile, N-octanoylcaprolactam (OCL) and N-methylpiperazin-N, N'-diacetonitrile as well as liquid or poorly crystallizing bleach activators in a form made up as a solid product. bleach stabilizer

These are additives that can adsorb, bind or complex heavy metal traces. Examples of additives with bleach-stabilizing action which can be used according to the invention are polyanionic compounds such as polyphosphates, polycarboxylates, polyhydroxypolycarboxylates, soluble silicates as completely or partially neutralized alkali or alkaline earth metal salts, in particular as neutral Na or Mg salts, which are relatively weak bleach stabilizers. Strong bleach stabilizers which can be used according to the invention are, for example, complexing agents, such as ethylenediaminetetraacetate (EDTA), nitrilotriacetic acid (NTA), methylglycinediacetic acid (MGDA), ß-alaninediacetic acid (ADA), ethylenediamine-N, N'-disuccinate (EDDS) and phosphonates, such as ethylenediophosphidenetronate, such as ethylenediophosphidenataminonate, such as ethylenediaminophosphonate, or ethylenediophosphonate diamine amine, -l, l-diphosphonic acid in foπn the acids or as partially or completely neutralized alkali metal salts. The complexing agents are preferably used in the form of their Na salts.

In the field of textile washing, bleaching and cleaning in the household and in the commercial sector, the bleaching or textile detergent compositions described according to one embodiment of the invention can contain almost all of the usual constituents of washing, bleaching and cleaning agents. In this way it is possible, for example, to build up means which are particularly suitable for textile treatment at low temperatures, and also means which are suitable in a number of temperature ranges up to the traditional area of cooked laundry.

In addition to bleaching agent compositions, the main components of textile washing and cleaning agents are builders, ie inorganic builders and or organic cobuilders, and surfactants, in particular anionic and / or nonionic surfactants. In addition, other customary auxiliaries and accompanying substances such as bulking agents, complexing agents, phosphonates, dyes, corrosion inhibitors, graying inhibitors and / or soil release polymers, color transfer inhibitors, bleaching catalysts, peroxide stabilizers, electrolytes, optical brighteners, enzymes, paxfum oils, foam regulators and activating agents available if this is appropriate. Inorganic builders (builders)

All conventional inorganic builders such as aluminosilicates, silicates, carbonates and phosphates are suitable as inorganic builder substances.

Suitable inorganic builders are e.g. Alumosilicates with ion exchange properties such as Zeolites. Different types of zeolites are suitable, in particular zeolite A, X, B, P, MAP and HS in their Na form or in forms in which Na is partly replaced by other cations such as Li, K, Ca, Mg or ammonium. Suitable zeolites are described, for example, in EP-A 038 591, EP-A 021 491, EP-A 087 035, US-A 4,604,224, GB-A2 013 259, EP-A 522 726, EP-A 384 070 and WO-A 94/24 251.

Other suitable inorganic builders are e.g. amorphous or crystalline silicates such as e.g. amorphous disilicates, crystalline disilicates such as the layered silicate SKS-6 (manufacturer Hoechst). The silicates can be used in the form of their alkali, alkaline earth or ammonium salts. Na, Li and Mg silicates are preferably used.

Anionic surfactants

Suitable anionic surfactants are the linear and / or slightly branched alkylbenzenesulfonates (LAS) according to the invention.

Other suitable anionic surfactants are, for example, fatty alcohol sulfates of fatty alcohols having 8 to 22, preferably 10 to 18 carbon atoms, for example C -Cπ alcohol sulfates, C ₁₂ -C ₁₃ alcohol sulfates, cetyl sulfate, myristyl sulfate, palmityl sulfate, stearyl sulfate and tallow fatty alcohol sulfate.

Other suitable anionic surfactants are sulfated ethoxylated C ₈ -C ₂₂ alcohols (alkyl ether sulfates) or their soluble salts. Compounds of this type are prepared, for example, by first alkoxylating a C ₈ -C ₂₂ , preferably a C ₁₈ -C ₁₈ alcohol, for example a fatty alcohol, and then sulfating the alkoxylation product. Ethylene oxide is preferably used for the alkoxylation, 2 to 50, preferably 3 to 20, mol of ethylene oxide being used per mol of fatty alcohol. However, the alkoxylation of the alcohols can also be carried out using propylene oxide alone and, if appropriate, butylene oxide. Also suitable are those alkoxylated Cs-C ^ alcohols, the ethylene oxide and propylene oxide or ethylene oxide and Contain butylene oxide. The alkoxylated C ₈ to C ₂₂ alcohols can contain the ethylene oxide, propylene oxide and butylene oxide units in the form of blocks or in statistical distribution.

Further suitable anionic surfactants are, preferably, N-acyl sarcosinates with aliphatic saturated or unsaturated C ₈ -C ₂₅ -acyl radicals z. B. N-oleoyl sarcosinate.

The amonic surfactants are preferably added to the detergent in the form of salts. Suitable cations in these salts are alkali metal salts such as sodium, potassium and lithium and ammonium salts such as e.g. Hydroxyethylammonium, di (hydroxyethyl) ammonium and tri (hydroxyethyl) ammonium salts.

The detergents according to the invention preferably contain Cio-Cu linear and / or - slightly branched alkylbenzenesulfonates (LAS).

Nonionic surfactants

Examples of suitable nonionic surfactants are alkoxylated C ₈ -C ₂₂ alcohols, such as fatty alcohol alkoxylates or oxo alcohol alkoxylates. The alkoxylation can be carried out using ethylene oxide, propylene oxide and / or butylene oxide. All alkoxylated alcohols which contain at least two molecules of an alkylene oxide mentioned above can be used as the surfactant. Here too, block polymers of ethylene oxide, propylene oxide and / or butylene oxide come into consideration or addition products which contain the alkylene oxides mentioned in a statistical distribution. 2 to 50, preferably 3 to 20, mol of at least one alkylene oxide are used per mole of alcohol. Ethylene oxide is preferably used as the alkylene oxide. The alcohols preferably have 10 to 18 carbon atoms.

Another class of suitable nonionic surfactants are alkylphenol ethoxylates with C ₆ -C ₁₄ alkyl chains and 5 to 30 mol ethylene oxide units.

Another class of nonionic surfactants are alkyl polyglucosides with 8 to 22, preferably 10 to 18 carbon atoms in the alkyl chain. These compounds usually contain 1 to 20, preferably 1.1 to 5, glucoside units. Another class of nonionic surfactants are N-alkyl glucamides of general structure II or III

R ⁷

I

R ⁶ -C- -NN - FR ⁸ (II) R ⁶ -NCR ^s (III) ι 7I I

0 RΌ

wherein R ^{6 is} C ₆ -C ₂₂ alkyl, R7 H or - alkyl and R8 is a polyhydroxyalkyl radical having 5 to 12 carbon atoms and at least 3 hydroxy groups. R _{6 is} preferably C ₁ -C ₁₈ -alkyl, R ^{7 is} methyl and R ^{8 is} a C ₅ - or C ₆ -rest. For example, such compounds are obtained by the acylation of reducing aminated sugars with acid chlorides of o-cig carboxylic acids.

Organic cobuilder

Suitable low molecular weight polycarboxylates as organic cobuilders are, for example: C ₄ -C o-di-, tri- and tetracarboxylic acids such as succinic acid, propane tricarboxylic acid, butane tetracarboxylic acid, cyclopentane tetracarboxylic acid and alkyl and alkenyl succinic acids with C ₂ -C ₆ alkyl or- alkenyl radicals;

C -C ₂₀ hydroxycarboxylic acids such as malic acid, tartaric acid, gluconic acid, glucaric acid, citric acid, lactobionic acid and sucrose mono-, di- and tricarboxylic acid;

Aminopolycarboxylates such as e.g. Nitrilotriacetic acid, methylglycinediacetic acid, alaninediacetic acid, ethylenediaminetetraacetic acid and serinediacetic acid;

Salts of phosphonic acids such as e.g. Hydroxyethane diphosphonic acid, ethylenediammetetta (me ylenphosphonate) and diethylenetriammpenta (methylenephosphonate)

Examples of suitable oligomeric or polymeric polycarboxylates as organic cobuilders are: Oligomaleic acids as described, for example, in EP-A-451 508 and EP-A-396 303;

Copolymers and terpolymers of unsaturated C ₄ -C ₈ dicarboxylic acids, with monoethylenically unsaturated monomers as comonomers

from the group (i) in amounts of up to 95% by weight from the group (ii) in amounts of up to 60% by weight from the group (iii) in amounts of up to 20% by weight copolymerized could be.

Examples of suitable unsaturated C ₄ -C ₈ dicarboxylic acids are maleic acid, fumaric acid, itaconic acid and citraconic acid. Maleic acid is preferred.

Group (i) includes monoethylenically unsaturated C ₃ -C ₈ -monocarboxylic acids such as acrylic acid, methacrylic acid, crotonic acid and vinyl acetic acid. From group (i), preference is given to using acrylic acid and methacrylic acid.

Group (ii) includes monoethylenically unsaturated C ₂ -C ₂₂ -01efins, vinyl alkyl ethers with - C ₈ -alkyl groups, styrene, vinyl esters of Ci-C ₈ carboxylic acids, (meth) acrylamide and vinyl pyrrolidone. From group (ii), preference is given to using C ₂ -C ₆ -01efins, vinyl alkyl ethers with -Gralkyl groups, vinyl acetate and vinyl propionate.

Group (iii) includes (meth) acrylic esters of -Cs alcohols, (meth) acrylonitrile, (meth) acrylamides of C _ϊ -Cs amines, N-vinylformamide and vinylimidazole.

If the polymers of group (ii) contain vinyl esters in copolymerized form, these can also be partially or completely hydrolyzed to vinyl alcohol units. Suitable copolymers and terpolymers are known, for example, from US Pat. No. 3,887,806 and DE-A43 13 909.

Suitable copolymers of dicarboxylic acids as organic cobuilders are preferably:

Copolymers of maleic acid and acrylic acid in a weight ratio of 10:90 to 95: 5, particularly preferably those in a weight ratio of 30:70 to 90:10 with molecular weights of 10,000 to 150,000; Terpolymers of maleic acid, acrylic acid and a vinyl ester of a -Cs carboxylic acid in a weight ratio of 10 (maleic acid): 90 (acrylic acid + vinyl ester) to 95 (maleic acid): 5 (acrylic acid + vinyl ester), the weight ratio of acrylic acid to vinyl ester in Range can vary from 20:80 to 80:20, and particularly preferred

Terpolymers of maleic acid, acrylic acid and vinyl acetate or vinyl propionate in a weight ratio of 20 (maleic acid): 80 (acrylic acid + vinyl ester) to

90 (maleic acid): 10 (acrylic acid + vinyl ester), the weight ratio of acrylic acid to vinyl ester varying in the range from 30:70 to 70:30;

Copolymers of maleic acid with C ₂ -C ₈ -olefins in a molar ratio of 40:60 to 80:20, copolymers of maleic acid with ethylene, propylene or isobutane in a molar ratio of 50:50 being particularly preferred.

Graft polymers of unsaturated carboxylic acids on low molecular weight carbohydrates or hydrogenated carbohydrates, cf. US-A 5,227,446, DE-A-44 15 623, DE-A-43 13 909 are also suitable as organic cobuilders.

Suitable unsaturated carboxylic acids are, for example, maleic acid, fumaric acid, itaconic acid, citraconic acid, acrylic acid, methacrylic acid, crotonic acid and Nmylacetic acid and mixtures of acrylic acid and maleic acid, which are grafted on in amounts of 40 to 95% by weight, based on the component to be grafted.

For modification, up to 30% by weight, based on the component to be grafted, of additional monoethylenically unsaturated monomers may be present in copolymerized form. Suitable modifying monomers are the above-mentioned monomers of groups (ii) and (iii).

Degraded polysaccharides such as acidic or enzymatically degraded starches, inulins or cellulose, reduced (hydrogenated or hydrogenated aminated) degraded polysaccharides such as mannitol, sorbitol, aminosorbitol and glucamine and polyalkylene glycols with molar masses of up to M _w = 5,000 such as polyethylene glycols are suitable as the graft base. Ethylene oxide / propylene oxide or ethylene oxide butylene oxide block copolymers, statistical ethylene oxide / propylene oxide or ethylene oxide butylene oxide copolymers, alkoxylated mono- or polybasic C 1 -C ₂₂ alcohols, cf. US-A 4,746,456. From this group, grafted degraded or degraded reduced starches and grafted polyethylene oxides are preferably used, 20 to 80% by weight of monomers based on the graft component being used in the graft polymerization. A mixture of maleic acid and acrylic acid in a weight ratio of 90:10 to 10:90 is preferably used for the grafting.

Polyglyoxylic acids as organic cobuilders are described, for example, in EP-B-001 004, US-A 5,399,286, DE-A-41 06 355 and EP-A-656 914. The end groups of the polyglyoxylic acids can have different structures.

Polyamidocarboxylic acids and modified polyamidocarboxylic acids as organic cobuilders are known, for example, from EP-A-454 126, EP-B-511 037, WO-A 94/01486 and EP-A-581 452.

Polyaspartic acid or co-condensates of aspartic acid with further amino acids, C -C ₂₅ -mono- or - dicarboxylic acids and / or C -C ₂ s -mono- or -diamines are also preferably used as organic cobuilders. Are particularly preferred in phosphorus-containing acids prepared with C _ö C22-mono- or -dicarboxylic acids or with C ₆ - C ₂₂ used modified mono- or diamines, polyaspartic acids.

Condensation products of citric acid with hydroxycarboxylic acids or polyhydroxy compounds as organic cobuilders are e.g. known from WO-A 93/22362 and WO-A 92/16493. Such condensates containing carboxyl groups usually have molecular weights of up to 10,000, preferably up to 5,000.

Graying inhibitors and soil release polymers

Suitable soil release polymers and / or graying inhibitors for detergents are, for example:

Polyesters of polyethylene oxides with ethylene glycol and / or propylene glycol and aromatic dicarboxylic acids or aromatic and aliphatic dicarboxylic acids;

Polyester made of polyethylene oxides end capped on one side with di- and / or polyhydric alcohols and dicarboxylic acid. Such polyesters are known, for example from US-A 3,557,039, GB-A 1 154 730, EP-A-185 427, EP-A-241 984, EP-A-241 985, EP-A-272 033 and US-A 5,142,020.

Other suitable soil-release polymers are amphiphilic graft or copolymers of vinyl and / or acrylic esters on polyalkylene oxides (cf. US Pat. No. 4,746,456, US Pat. No. 4,846,995, DE-A-37 11 299, US Pat. No. 4,904,408, US Pat. A 4,846,994 and US-A 4,849,126) or modified celluloses such as Methyl cellulose, hydroxypropyl cellulose or carboxymethyl cellulose.

Color transfer inhibitors

Color transfer inhibitors used, for example, are homopolymers and copolymers of vinylpyrrolidone, vinylimidazole, vinyloxazolidone and 4-vinylpyridine-N-oxide with molecular weights from 15,000 to 100,000, and crosslinked, finely divided polymers based on these monomers. The use of such polymers mentioned here is known, cf. DE-B-22 32 353, DE-A-28 14287, DE-A-28 14 329 and DE-A-43 16 023.

enzymes

Suitable enzymes are, for example, proteases, amylases, lipases and cellulases, in particular proteases. Several enzymes can be used in combination.

In addition to the use in detergents and cleaning agents for textile laundry in the household, the detergent compositions which can be used according to the invention can also be used in the field of commercial textile washing and cleaning. As a rule, peracetic acid is used as a bleaching agent in this area of application, which is added to the wash liquor as an aqueous solution.

Use in laundry detergents

A typical powder or granular heavy-duty detergent according to the invention can have the following composition, for example:

0.5 to 50% by weight, preferably 5 to 30% by weight, of at least one anionic and / or nonionic surfactant, 0.5 to 60% by weight, preferably 15 to 40% by weight, at least an inorganic builder, 0 to 20% by weight, preferably 0.5 to 8% by weight, of at least one organic cobuilders,

2 to 35% by weight, preferably 5 to 30% by weight, of an inorganic bleaching agent, 0.1 to 20% by weight, preferably 0.5 to 10% by weight, of a bleach activator, optionally in a mixture with others bleach activators,

0 to 1% by weight, preferably up to at most 0.5% by weight, of a bleaching catalyst, 0 to 5% by weight, preferably 0 to 2.5% by weight, of a polymeric color transfer inhibitor,

0 to 1.5% by weight, preferably 0.1 to 1.0% by weight, protease, 0 to 1.5% by weight, preferably 0.1 to 1.0% by weight, lipase .

0 to 1.5% by weight, preferably 0.2 to 1.0% by weight of a soil release polymer,

ad 100% usual auxiliary and accompanying substances and water.

Inorganic builders which are preferably used in detergents are sodium carbonate, sodium hydrogen carbonate, zeolite A and P and amorphous and crystalline Na silicates.

Organic cobuilders preferably used in detergents are acrylic acid / maleic acid copolymers, acrylic acid / maleic acid / vinyl ester terpolymers and citric acid.

Inorganic bleaching agents preferably used in detergents are sodium perborate and sodium carbonate perhydrate.

The anionic surfactants preferably used in detergents are the linear and slightly branched alkylbenzenesulfonates (LAS), fatty alcohol sulfates and soaps according to the invention.

Nonionic surfactants preferably used in detergents are Cπ-C ₁₇ - oxo alcohol ethoxylates with 3-13 ethylene oxide units, C _ϊö -Ci _ö fatty alcohol ethoxylates with 3- 13 ethylene oxide units and additionally ethoxylated fat or alkoxylated with 1-4 propylene oxide or butylene oxide units oxo alcohols.

Enzymes which are preferably used in detergents are protease, lipase and cellulase. Of the commercially available enzymes, amounts of 0.05 to 2.0% by weight, preferably 0.2 to 1.5% by weight, of the made-up enzyme are generally added to the detergent.

Suitable proteases are, for example, Savinase, Desazym and Esperase (manufacturer Novo Nordisk). A suitable lipase is, for example, Lipolase (manufacturer Novo Nordisk). A suitable cellulase is eg Celluzym (manufacturer Novo Nordisk).

Graying inhibitors and soil release polymers preferably used in detergents are graft polymers of vinyl acetate on polyethylene oxide of molecular weight 2,500-8,000 in a weight ratio of 1.2: 1 to 3.0: 1.

Polyethylene terephthalates / oxyethylene terephthalates with a molecular weight of 3,000 to 25,000 made from polyethylene oxides with a molecular weight of 750 to 5,000 with terephthalic acid and ethylene oxide and a molar ratio of polyethylene terephthalate to polyoxyethylene terephthalate of 8: 1 to 1: 1 and block polycondensates according to DE-A-44 03 866.

Color transfer inhibitors preferably used in detergents are soluble vinylpyrrolidone and vinylimidazole copolymers with molecular weights above 25,000 and finely divided crosslinked polymers based on vinylimidazole.

The powdered or granular detergents according to the invention can contain up to 60% by weight of inorganic fillers. Sodium sulfate is usually used for this. However, the detergents according to the invention are preferably low in adjusting agents and contain only up to 20% by weight, particularly preferably only up to 8% by weight, of adjusting agents.

The detergents according to the invention can have different bulk densities in the range from 300 to 1,200, in particular 500 to 950 g / l. Modern compact detergents generally have high bulk densities and show a granular structure.

The invention is illustrated by the examples below.

example 1

A butadiene-free C ₄ fraction with a total butene content of 84.2% by weight and a molar ratio of 1-butene to 2-butenes of 1 to 1.06 is continuously at 40 ° C and 10 bar over a with Re ₂ θ ₇ / Al ₂ 0 ₃ heterogeneous contact equipped tube reactor. In the example, the catalyst load is 4500 kg / m ² h. The reaction discharge is separated by distillation and contains the following components (data in percent by mass): ethene 1.15%; Propene 18.9%, butane 15.8%, 2-butene 19.7%, 1-butene 13.3%, i-butene 1.0%, 2-pentene 19.4%, methylbutene 0.45%, 3-hexene 10.3%. 2-pentene and 3-hexene are obtained from the product by distillation in purities> 99% by weight.

Example 2

Continuous dimerization of 3-witches in a fixed bed process

Catalyst: 50% NiO, 34% Si0 ₂ , 13% TiO ₂ , 3% Al ₂ O ₃ (according to DE 43 39 713) used as 1-1.5 mm grit (100 ml), 24 h at 160 ° C in N ₂ conditioned

Reactor: isothermal, 16 mm 0 reactor WHSV: 0.25 kg / l.h

Pressure: 20 to 25 bar

Temperature: 100 to 160 ° C

The collected product was distilled to a C ₁₂ purity of 99.9% by weight and the framework isomers of the C ₂ fraction were determined (14.2% n-dodecenes, 31.8% 5-methylundecenes ₅ 29 , 1% 4-ethyldecenes, 6.6% 5,6-dimethyldecenes, 9.3% 4-

Methyl 5-ethylnonenes, 3.7% 4,5-diethyloctenes, figures in% by weight).

Example 3

2-pentene from the raffinate II metathesis was dimerized analogously to Example 2 on a Ni-hetrogen catalyst. A decene fraction with a purity of 99.5% was obtained by fractional distillation of the product.

1 H-NMR spectroscopy determined an iso index of 1.36 after hydrogenation of the olefin. The hydrogenated sample was then analyzed by gas chromatography for the skeletal isomers of the paraffins. (n-decane 13.0%, 4-methyl-nonane 26.9%, 3-ethyloctane 16.5%, 4,5-dimethyloctane 5.4%, 3,4-diethylhexane 6.8%, 3-ethyl-4 - methylheptane 9.2%, (figures in% by weight)). The sample contains 22% C 10 paraffms of unassignable structure.

Example 4

A mixture of 2-pentene and 3-hexes from the raffinate II metathesis was continuously dimerized analogously to Example 2 and Example 3. Fractional distillation of the product gave a decen / undecen / dodecene fraction with a purity of 99.5%. Example 5 (comparison)

In a 6 L reactor were 39.2 g and 6458g benzene A1C1 ₃ and adding, with stirring 1393g of a C ₁₂ -01efmgemisches according to Example 2 are metered. The reaction temperature of 20 ° C was regulated by cooling in an ice bath and by varying the metering rate of the olefin mixture. After 55 min the reaction mixture was decanted, neutralized with NaOH and washed with demineralized water. This was followed by filtration and drying using round and cotton filters. The LAB yield was 83.4%. The alkylbenzene mixture consisted of 56% PhCHRR ', 44% PhCRR'R''and 0% PhCH ₂ R.

Example 6

1900 g of S03-depleted oleum are placed in a 2 L four-necked flask with magnetic stirrer, thermometer, dropping funnel, gas inlet frit and gas outlet. This flask is connected to a 1 L three-neck flask via a Viton tube via the gas outlet.

In this 1 L flask with blade stirrer, thermometer, gas inlet frit and gas outlet, an alkylbenzene mixture similar to Example 5 is placed.

The depleted oleum is brought to 120 ° C. in the SO ₃ developer and the oleum (65%) is added via a dropping funnel within 30 minutes. The SO ₃ gas is stripped off with a nitrogen stream of 80 L / h and introduced into the alkylbenzene via a 6 mm inlet pipe. The temperature of the alkylbenzene / alkylbenzenesulfonic acid mixture slowly rises to 40 ° C. and is kept at 40 ° C. with cooling water. The residual gas is drawn off via a water jet pump.

The molar ratio of SO ₃ / alkylbenzene is 1.01: 1.

The alkylbenzene sulfonic acid formed is stabilized after a reaction time of 4 hours with 0.4% by weight of water and then neutralized with NaOH to give the alkylbenzene sulfonate.

Example 7

12,75g HY zeolite (Si: Al = 5.58: 1 molar) 5h was dried at 500 ° C together with 120 g benzene, 25.5 g of a C ₁₂ -01efmgemisches according to Example 2 in a 300 ml of steel autoclaves stirred at 180 ° C. under N _{2 for} 6 h. The zeolite was then separated off and the product mixture was analyzed by means of GC (column DB-5, 50 m). It consisted of 87.1% benzene, 3.7% unreacted C ₂ olefm, 7.6% dodecylbenzene and <0.1% heavy alkylate (dialkylbenzenes) in addition to small amounts of unidentified hydrocarbons.

The product mixture was distilled at 1 mbar in vacuo. Between 130 ° C and 150 ° C, 9.5 g of an alkylbenzene mixture consisting of 97% PhCHRR ', 0% PhCRR'R "and 3% PhCH ₂ R were obtained.

Example 8

An alkylbenzene mixture analogous to Example 7 was converted to the alkylbenzenesulfonate as described in Example 6.

Example 9 (comparison)

12.75 g of H-MOR zeolite (Si: Al = 24.5: 1 molar) was dried at 500 ° C. for 5 hours and together with 120 g of benzene, 25.5 g of a C 1-4 olefin mixture according to Example 2 in a 300 ml steel autoclave for 6 hours stirred at 180 ° C under N ₂ . The zeolite was then separated off and the product mixture was analyzed by means of GC (column DB-5, 50 m). It consisted of 85.1% benzene, 8.8% unreacted C ₁₂ olefin, 4.4% dodecylbenzene and <0.1% heavy alkylate (dialkylbenzenes) in addition to small amounts of unidentified hydrocarbons. The product mixture was distilled at 1 mbar in vacuo. Between 130 ° C and 150 ° C, 4.9 g of an alkylbenzene mixture consisting of 96% PhCHRR ', 2% PhCRR'R "and 2% PhCH ₂ R were obtained.

Example 10 (comparison)

12.75 g of H-ZSM-5 zeolite (Si: Al = 42.5: 1 molar) was dried for 5 hours at 500 ° C. and together with 120 g of benzene, 25.5 g of a C ₁₂ -olefin mixture according to Example 2 in a 300 ml Steel autoclave stirred for 6h at 180 ° C under N ₂ . The zeolite was then separated off and the product mixture was analyzed by means of GC (column DB-5, 50 m). It consisted of 88.6% benzene, 7.1% unreacted C ₁₂ olefin, 1.0% dodecylbenzene and <0.1% heavy alkylate (dialkylbenzenes) in addition to small amounts of unidentified hydrocarbons. Example 11 (comparison)

12.75 g of H-MCM-22 zeolite (Si: Al = 18.8: 1 molar) was dried at 500 ° C. for 5 hours and together with 120 g of benzene, 25.5 g of a C ₁₂ olefin mixture according to Example 2 in a 300 ml Steel autoclave stirred at 180 ° C under N2 for 6h. The zeolite was then separated off and the product mixture was analyzed by means of GC (column DB-5, 50 m). It consisted of 87.1% benzene, 5.6% unreacted C ₂ olefm, 6.7% dodecylbenzene and <0.1% heavy alkylate (dialkylbenzenes) in addition to small amounts of unidentified hydrocarbons.

The product mixture was distilled at 1 mbar in vacuo. 8.4 g of an alkylbenzene mixture consisting of 73% PhCHRR ', 23% PhCRR'R "and 4% PhCH ₂ R were obtained between 130 ° C and 150 ° C.

Example 12

12.75 g of HY zeolite (Si: Al = 5.58: 1 molar) was dried at 500 ° C. for 5 hours and together with 120 g of benzene, 25.5 g of a CIO-olefin mixture according to Example 3 in a 300 ml steel autoclave for 6 hours at 180 ° C stirred under N ₂ . The zeolite was then separated off and the product mixture was analyzed by means of GC (column DB-5, 50 m). The product showed the following isomer distribution: 96% PhCHRR ', 0% PhCRR'R "and 4% PhCH ₂ R.

Example 13

An alkylbenzene mixture analogous to Example 12 was converted to the alkylbenzenesulfonate as described in Example 6.

Example 14

12.75 g of HY zeolite (Si: Al = 5.58: 1 molar) was dried at 500 ° C. for 5 hours and together with 120 g of benzene, 25.5 g of a C ₁₀ -ι ₂ olefin mixture according to Example 4 in a 300 ml steel autoclave Stirred for 6h at 180 ° C under N ₂ . The zeolite was then separated off and the product mixture was analyzed by means of GC (column DB-5, 50 m). The product showed the following isomer distribution: 97% PhCHRR ', 1% PhCRR'R "and 2% PhCH ₂ R. Example 15

An alkylbenzene mixture analogous to Example 14 was converted to the alkylbenzenesulfonate as described in Example 6.

Example 16

IL / h oleum (65%) in concentrated sulfuric acid is introduced into a heated (120 ° C.) 10 L four-necked flask with a pump. Dry air, which strips the SO _{3, is} passed through the frit 1301 / h through the sulfuric acid. The air stream enriched with S0 ₃ (approx. 4% SO ₃ ) is brought into contact with an alkylbenzene mixture analogous to Example 7 in a 2m long falling film reactor at about 40-50 ° C (10-15 ° C double jacket water cooling) and this sulfonated. The molar ratio of SO ₃ / alkylbenzene is 1.01: 1. The reaction time in the falling film reactor is approximately 10 seconds. The product is pumped into a post-ripening tank where it stays for about 4-8 hours. The sulfonic acid is then stabilized with 0.4% by weight of water and neutralized with NaOH to give the alkylbenzenesulfonate.

Claims

claims

1. Process for the preparation of alkylaryl compounds

1) Production of a mixture of Cio- ₁₄ olefins, which are predominantly monobranched on average, by

a) reaction of a C ₄ -01efin mixture over a methathesis catalyst to produce an olefin mixture containing 2-pentene and / or 3-hexene and, if appropriate, separation of 2-pentene and / or 3-hexene, followed by dimerization of the 2- Pentens and / or 3-Hexens over a dimerization catalyst to a mixture containing Cio- _12- olefins and optionally separating the C ₁₀ -i ₂ -olefins, or

b) extraction of predominantly single-branched paraffins from kerosene cuts and subsequent dehydration, or

c) Fischer-Tropsch synthesis of olefins or paraffins, the paraffins being dehydrated, or

d) dimerization of short-chain internal olefins, or

e) isomerization of linear olefins or paraffins, the isomerized paraffins being dehydrated,

2) Reaction of the olefin mixture obtained in stage 1) with an aromatic

Hydrocarbon in the presence of an alkylation catalyst containing faujasite type zeolites.

2. A process for the preparation of alkylarylsulfonates by preparing alkylaryl compounds according to claim 1 and below

3) Sulfonation and neutralization of the alkylaryl compounds obtained in stage 2).

3. The method according to claim 1 or 2, characterized in that in stage la) the methathesis catalyst is selected from compounds of a metal of subgroups VIb, Vllb or VIII of the periodic table of the elements.

4. The method according to any one of claims 1 to 3, characterized in that in stage 2) the reaction conditions and the catalyst are selected so that the alkylaryl compounds obtained in the alkyl radical have 1 to 3 carbon atoms with an H / C index of 1 and the The proportion of carbon atoms with an H / C index of 0 in the alkyl radical is statistically less than 5%.

5. alkylaryl compounds obtainable by the process according to claim 1.

6. alkylarylsulfonates obtainable by the process according to claim 2.

7. Use of alkylarylsulfonates according to claim 6 as surfactants.

8. Use according to claim 7 in detergents and cleaning agents.

9. washing and cleaning agents containing alkylarylsulfonates according to claim 6 in addition to conventional ingredients.