Description

The present invention relates to a method for preparing an oligobutyl benzene sulfonate comprising the steps of oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, alkylation of benzene with the alkene blend to produce an oligobutyl benzene, sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and neutralizing the oligobutyl benzene sulfonic acid to produce the oligobutyl benzene sulfonate. The invention also relates to the oligobutyl benzene sulfonate obtainable by the method; to the oligobutyl benzene sulfonic acid obtainable by the method; to the oligobutyl benzene obtainable by the method; to the lubricant comprising the oligobutyl benzene sulfonate; to a fuel comprising the oligobutyl benzene sulfonate; and to a use of the oligobutyl benzene sulfonate as lubricant additive or fuel additive. Combinations of preferred embodiments with other preferred embodiments are within the scope of the present invention.

Alkylbenzene sulfonates are useful additives for lubricants and fuels. Objects were to overcome disadvantages and to find an improved synthesis of alkylbenzene sulfonates and improved lubricants or fuels containing the alkylbenzene sulfonates. Further objective was to improve lubricants, where the lubricant has good rheological behavior, a high viscosity index, a good low temperature performance (e.g. in the cold crankcase simulation), a low viscosity under operating conditions (e.g. in the high temperature high shear HTHS viscosity test), a high shear stability, or a low viscosity loss after many use cycles. Further objects were to find fuel or lubricant additives with a higher solubility. Further objects were to find lubricant additives and fuel additives which result in an improved storage stability, prevent precipitations, corrosion protection, improve formulability (e.g. mixability with other components of the mixtures), or filterability.

The objects were solved by a method for preparing an oligobutyl benzene sulfonate comprising the steps of i) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and iv) neutralizing the oligobutyl benzene sulfonic acid to produce the oligobutyl benzene sulfonate. The butene mix which can be used for oligomerization comprises 1 -butene and 2-butene. The 2-butene may be cis-2-butene, trans-2-butene, or mixtures thereof.

The butene mix may contain from 20 to 99 wt%, preferably from 50 to 99 wt%, and in particular from 70 to 95 wt%, based on the total olefin content, of 1 -butene and 2-butene.

The ratio of 1 -butene to 2-butene in the butene mix is usually in a range from 20 : 1 to 1 : 2, preferably 10 : 1 to 1 : 1.

The butene mix may comprise less than 5% by weight, in particular less than 3% by weight, of isobutene.

The butene mix is preferably obtainable from a raffinate II. An industrially available butene mix results usually from hydrocarbon cleavage during the processing of petroleum, for example by catalytic cracking, such as fluid catalytic cracking (FCC), thermocracking or hydrocracking with subsequent dehydration. A suitable industrial butene mix is the C4 cut, which is obtainable, for example, by fluid catalytic cracking or steam cracking of gas oil and/or by steam cracking naphtha.

Depending on the composition of the C4 cut, a distinction is made between the whole C4 cut (crude C4 cut), the so-called raffinate I obtained after separating off 1 ,3-butadiene, and the raffinate II obtained after separating off isobutene. Isobutene can be separated off from C4- olefin mixtures, such as raffinate I, by one of the following methods: molecular sieve separation, fractional distillation, reversible hydration to tert-butanol, acid-catalyzed alcohol addition onto a tertiary ether, e.g. methanol addition to methyl tert-butyl ether (MTBE), irreversible catalyzed oligomerization to di- and triisobutene or irreversible polymerization to polyisobutene.

The butene mix can be obtainable as crude C4 cut which is obtainable by fluid catalytic cracking or steam cracking of gas oil and/or by steam cracking naphtha.

The butene mix can be obtainable from the crude C4 cut.

The butene mix can be obtainable from the raffinate I, where the raffinate I is obtainable from the crude C4 cut after separating off 1 ,3-butadiene.

The butene mix can be obtainable from the raffinate II, where the raffinate II is obtainable from the raffinate I after separating off isobutene. The butene mix, which is for example obtainable as raffinate II, can comprise from 0.5 to 5% by weight of isobutane, from 5 to 20% by weight of n-butane, from 20 to 40% by weight of trans-2-butene, from 10 to 20% by weight of cis-2-butene, from 25 to 55% by weight of 1 -butene, and from 0.5 to 5% by weight of isobutene.

The butene mix may comprise trace gases, such as 1,3-butadiene, propene, propane, cyclopropane, propadiene, methylcyclopropane, vinylacetylene, pentenes, pentanes in the range of in each case at most 1% by weight. If diolefins or alkynes are present in the butene mix, then these can be removed from same prior to the oligomerization to preferably less than 100 ppm. They are preferably removed by selective hydrogenation, particularly preferably by a selective hydrogenation to a residual content of below 50 ppm.

A raffinate II has the following typical composition: isobutane: 3% by weight, n-butane: 15% by weight, isobutene: 2% by weight, 1 -butene: 30% by weight, trans-2-butene: 32% by weight, cis-2-butene: 18% by weight.

For the oligomerization of the butene mix, a reaction system can be used which comprises one or more, identical or different reactors. In the simplest case, a single reactor is used for the oligomerization. However, it is also possible to use two or more reactors which each have identical or different mixing characteristics. The individual reactors can optionally be divided one or more times by internals. If two or more reactors form the reaction system, then these can be connected with one another in any desired manner, e.g. in parallel or in series. In a suitable configuration, for example, a reaction system is used which consists of two reactors connected in series.

Suitable pressure-resistant reaction apparatuses for the oligomerization are reactors for gassolid and gas-liquid reactions, such as, for example, tubular reactors, stirred-tank reactors, gas circulation reactors, bubble columns etc., which can, if appropriate, be divided by internals. Preference is given to using tube-bundle reactors or shaft furnaces. If a heterogeneous catalyst is used for the oligomerization, then this can be arranged in one or more catalyst fixed beds. Here, it is possible to use different catalysts in different reaction zones. However, preference is given to using the same catalysts in all reaction zones. The temperature during the oligomerization reaction is generally in a range from about 20 to 280°C, preferably from 25 to 200°C, in particular from 30 to 140°C. The pressure during the oligomerization is generally in a range from about 1 to 300 bar, preferably from 5 to 100 bar and in particular from 20 to 70 bar. If the reaction system comprises more than one reactor, then these can have identical or different temperatures and identical or different pressures. Thus, for example, in the second reactor of a reactor cascade, a higher temperature and/or a higher pressure than in the first reactor can be established, e.g. in order to achieve as complete a conversion as possible.

In a special embodiment, the temperature and pressure values used for the oligomerization are chosen such that the olefin-containing feed material is liquid or in the supercritical state.

The oligomerization reaction is preferably carried out adiabatically. This term is understood below in the technical sense and not in the physicochemical sense. Thus, the oligomerization reaction generally proceeds exothermally such that the reaction mixture, upon flowing through the reaction system, for example a catalyst bed, experiences a temperature increase. Adiabatic reaction procedure is understood as meaning a procedure in which the amount of heat released in an exothermic reaction is taken up by the reaction mixture in the reactor and no cooling by cooling devices is used. Thus, the heat of reaction is dissipated with the reaction mixture from the reactor, apart from a residual fraction which is released to the surroundings by natural heat conduction and heat radiation from the reactor.

For the oligomerization a transition-metal-containing catalyst is used. These are preferably heterogeneous catalysts. Preference is given to using an oligomerization catalyst which comprises nickel. In this connection, preference is given to heterogeneous catalysts which comprise nickel oxide. The heterogeneous-nickel-comprising catalysts used can have various structures. Of suitability in principle are unsupported catalysts and also supported catalysts. The latter are preferably used. The support materials may be, for example, silica, clay earths, aluminosilicates, aluminosilicates with layer structures and zeolites, such as mordenite, faujasite, zeolite X, zeolite Y and ZSM-5, zirconium oxide which has been treated with acids, or sulfated titanium dioxide. Of particular suitability are precipitated catalysts which are obtainable by mixing aqueous solutions of nickel salts and silicates, e.g. sodium silicate with nickel nitrate, and if appropriate aluminum salts, such as aluminum nitrate, and calcining. Furthermore, it is possible to use catalysts which are obtained by incorporating Ni ²⁺ ions through ion exchange into natural or synthetic sheet silicates, such as montmorillonites. Suitable catalysts can also be obtained through impregnation of silica, clay earth or aluminosilicates with aqueous solutions of soluble nickel salts, such as nickel nitrate, nickel sulfate or nickel chloride, and subsequent calcination.

Catalysts comprising nickel oxide are preferred. Particular preference is given to catalysts which consist essentially of NiO, SiC>2, TiC>2 and/or ZrC>2 and also if appropriate AI2O3. Most preference is given to a catalyst which comprises, as essential active constituents, 10 to 70% by weight of nickel oxide, 5 to 30% by weight of titanium dioxide and/or zirconium dioxide, 0 to 20% by weight of aluminum oxide and, as remainder, silicon dioxide. Such a catalyst is obtainable through precipitation of the catalyst mass at pH 5 to 9 by adding an aqueous solution comprising nickel nitrate to an alkali metal waterglass solution which comprises titanium dioxide and/or zirconium dioxide, filtration, drying and heating at 350 to 650°C.

The catalyst is preferably present in piece form, e.g. in the form of tablets, e.g. having a diameter of from 2 to 6 mm and a height of from 3 to 5 mm, rings having an external diameter of e.g. 5 to 7 mm, a height of from 2 to 5 mm and a hole diameter of from 2 to 3 mm, or strands of varying length with a diameter of e.g. 1.5 to 5 mm. Such forms are obtained in a manner known per se by tableting or extrusion, mostly using a tableting auxiliary, such as graphite or stearic acid.

The raw product of the oligomerization may be enriched by distillation. Distillative separation of the oligomerization product can be carried out continuously or batchwise (discontinuously).

Suitable distillation devices are the customary apparatuses known to the person skilled in the art. These include, for example, distillation columns, such as plate columns, which if desired can be equipped with internals, valves, sidestream takeoffs, etc., evaporators, such as thin- film evaporators, falling-film evaporators, wiper-blade evaporators, Sambay evaporators etc. and combinations thereof. Preferably, the C -olefin fraction is isolated by fractional distillation. The distillation can take place in one or more distillation columns coupled together.

The distillation columns used can comprise separating internals, such as separating trays, e.g. perforated trays, bubble-cap trays or valve trays, structured packings, e.g. sheet-metal and fabric packings, or random beds of packings. In the case of the use of tray columns with downcomers, the downcomer residence time is preferably at least 5 seconds, particularly preferably at least 7 seconds. Suitable evaporators and condensers are likewise apparatus types known per se. As evaporator, it is possible to use a heatable vessel customary for this purpose or an evaporator with forced circulation, for example a falling-film evaporator. If two distillation columns are used for the distillation, then these can be provided with identical or different evaporators and condensers.

Preferably, the bottom temperatures arising during the distillation are at most 300°C, particularly preferably at most 250°C. To maintain these maximum temperatures, the distillation can if desired be carried out under a suitable vacuum.

The oligomerization of the butene mix produces an alkene blend, which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol. The alkene blend is preferably obtainable by oligomerization in the presence of a nickel containing heterogenous catalyst.

The oligobutenes may have a molecular weight from 220 to 1000 g/mol, 220 to 700 g/mol, 220 to 500 g/mol, or 220 to 350 g/mol. The molecular weight can be determined by GPC using polystyrene standards, e.g. as described in DIN 55672-1. The molecular weight can be determined by gas chromatography coupled to mass spectrometry GC-MS. The molecular weight can be determined by HPLC coupled to mass spectrometry HPLC-MS.

The alkene blend may comprise at least 40 wt%, 50 wt%, 60 wt% or 80 wt% of the oligobutenes with a molecular weight of 220 to 2000 g/mol. In another form the alkene blend may comprise at least 40 wt%, 50 wt%, 60 wt% or 80 wt% of the oligobutenes with a molecular weight of 220 to 1000 g/mol. In another form the alkene blend may comprise at least 40 wt%, 50 wt%, 60 wt% or 80 wt% of the oligobutenes with a molecular weight of 220 to 500 g/mol. In another form the alkene blend may comprise at least 40 wt%, 50 wt%, 60 wt% or 80 wt% of the oligobutenes with a molecular weight of 220 to 350 g/mol.

The alkene blend comprises typically C alkenes, C20 alkenes, and C24 alkenes. The alkene blend comprises typically C alkenes, C20 alkenes, and C24 alkenes in a total amount of at least 20, 30, 40, 50, 60, 70, 80 or 90 wt%. The alkene blend comprises preferably C alkenes, C20 alkenes, and C24 alkenes in a total amount of at least 45 wt%. In another form the alkene blend comprises preferably C alkenes, C20 alkenes, and C24 alkenes in a total amount of at least 55 wt%.

The alkene blend may comprise terminal unsaturated oligobutenes, such as terminal unsaturated C alkenes, terminal unsaturated C20 alkenes, and terminal unsaturated C24 alkenes. The term “terminal unsaturated alkene” usually refers to a 1 -alkene (e.g. 1- hexadecene). The alkene blend may comprise at least 5 wt%, 15 wt%, 25 wt% or 35 wt% of the terminal unsaturated oligobutenes.

The alkene blend may comprise beta unsaturated oligobutenes, such as beta unsaturated Cie alkenes, beta unsaturated C20 alkenes, and beta unsaturated C24 alkenes. The term “beta unsaturated alkene” usually refers to a 2-alkene, e.g. 2-hexadecene. The alkene blend may comprise at least 5 wt%, 15 wt%, 25 wt% or 35 wt% of the beta unsaturated oligobutenes.

The alkene blend may comprise terminal and beta unsaturated oligobutenes, such as terminal and beta unsaturated Cis alkenes, terminal and beta unsaturated C20 alkenes, and terminal and beta unsaturated C24 alkenes. The alkene blend may comprise a total of at least 10 wt%, 30 wt%, 50 wt% or 70 wt% of the terminal and the beta unsaturated oligobutenes.

The alkene blend may comprise a mixture of linear and branched oligobutenes, such as a mixture of linear and branched Cis alkenes, a mixture of linear and branched C20 alkenes, and a mixture of linear and branched C24 alkenes. The branching of the oligobutene usually depends on the butene mix which was oligomerized. The butene mix may comprise less than 20 wt%, 15 wt%, 10 wt%, or 5 wt% of isobutene. The alkene blend may comprise less than 5 wt%, 3 wt%, 1 wt%, 0.5 wt% or 0.1 wt% oligoisobutenes. In another form the alkene blend may comprise less than 5 wt%, 3 wt%, 1 wt%, 0.5 wt% or 0.1 wt% oligoisobutenes with a molecular weight of above 220 g/mol. In another form the alkene blend is essentially free of oligoisobutenes. In another form the alkene blend is essentially free of oligoisobutenes with a molecular weight of above 220 g/mol.

The alkene blend may comprise a mixture of terminal unsaturated, linear and branched oligobutenes, such as a mixture of terminal unsaturated linear and branched Cis alkenes, a mixture of terminal unsaturated linear and branched C20 alkenes, and a mixture of terminal unsaturated linear and branched C24 alkenes.

The alkene blend may comprise lower oligobutenes, which are oligobutenes with a molecular weight below 220 g/mol, such as C12 alkenes or Cs alkenes. The alkene blend preferably comprises lower oligobutenes which are selected from C12 alkenes. The alkene blend may comprises up to 60, 50, 45, or 40 wt% of the lower oligobutenes, such as the C12 alkenes. The alkene blend may comprises 0.1 to 60, 1 to 50, 10 to 45 wt%, or 20 to 45 wt% of the lower oligobutenes, such as the C12 alkenes. The lower oligobutenes are usually terminal unsaturated alkenes, such as terminal unsaturated Cs alkenes or terminal unsaturated alkenes C12 alkenes. The alkene blend usually comprises

20 - 85 wt% of the C alkenes,

5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes.

In another form the alkene blend comprises

20 - 85 wt% of the C alkenes,

5 - 30 wt% of the C20 alkenes,

2 - 20 wt% of the C24 alkenes, and optionally further oligobutenes with a molecular weight of 220 to 2000 g/mol.

In another form the alkene blend comprises

20 - 85 wt% of the C alkenes,

5 - 30 wt% of the C20 alkenes,

2 - 20 wt% of the C24 alkenes, and optionally lower oligobutenes, such as C12 alkenes.

In another form the alkene blend comprises

20 - 85 wt% of the C alkenes,

5 - 30 wt% of the C20 alkenes,

2 - 20 wt% of the C24 alkenes, and optionally further oligobutenes with a molecular weight of 220 to 2000 g/mol, and optionally lower oligobutenes, such as C12 alkenes.

In another form the alkene blend comprises

20 - 85 wt% of the C alkenes,

5 - 30 wt% of the C20 alkenes,

2 - 20 wt% of the C24 alkenes,

20 - 60 wt% of the C12 alkenes, and optionally further oligobutenes with a molecular weight of 220 to 2000 g/mol.

The oligobutyl benzene is usually produced by alkylation of benzene with the alkene blend. The alkylation is usually a Friedel Crafts type reaction, in which typically an alkylation catalyst is used to catalyze an electrophilic aromatic substitution of an alkylating agent (e.g. an alkyl halide or alkene) to an aromatic ring. Suitable alkylation catalysts for the alkylation are heterogeneous acids, hydrofluoric acid, aluminum chloride, or boron fluoride, where heterogeneous acids are preferred. Suitable alkylation catalysts for the alkylation are heterogeneous acids selected from clays, in particular montmorillonite or montmorillonite-containing materials, such as, for example, K10 and K20 from Sudchemie, strongly acidic ion exchangers, such as Amberlyst® 36 or Amberlyst® 15 from Rohm & Haas or Nation® or Nafion®/silica from DuPont, acidic metal oxides, such as, for example, M(I)O3-M(II)C>2- M(I)=W, Mo and M(l I) = Zr,

Ti, Mn and/or Sn, AhCh-SiC^, TiO2-ZrO2, TiC>2, Nb20s, Ta2Os, sulfated metal oxides, such as ZrO2-SOs, TiO2-SOs, AI2O3-SO3, WO3-SO3, Nb2Os-SO3, supported heteropolyacids, such as PWi2-HPA/SiC>2, PMoi2-HPA/coal, P2Wi8-HPA/TiC>2, and zeolites.

Preferred alkylation catalysts for the alkylation are zeolites.

Preference is given to zeolites of the structure types BIK; BRE, ERI, CHA, DAC, EAB, EDI, EPI, FER, pentasils with MFI or MEL structure, faujasites, such as, for example, Y, LTL, MOR, BEA, GME, HEU, KFI, MAZ, OFF, PAU, RHO, STI. Particular preference is given to L, Y including the USY types, BEA and MOR. These zeolites are preferably used in the H and/or La form, although traces of Na, K, Mg or Ca may be present depending on the preparation. Partial or complete exchange of the lattice aluminum by B, Ga or Fe is possible.

The catalyst can be used directly as fine powder in suspension, in the case of zeolites, these are, for example, particle sizes between 100 nm and a few pm. However, in most cases, these catalysts are shaped together with binder materials to give shaped bodies with a diameter of 0.1-5 mm. For use in fixed beds, 1-3 mm are preferred, in suspension 0.001-1 mm, in moving beds 0.1-3 mm. Suitable binders are in particular clays, aluminum oxides, such as, for example, Purals, Sirals and Versals and silica gels. In addition, inert fillers such as SiO2 (e.g. Aerosil® from Degussa) can be added. Examples of suitable shaped bodies are tablets, small strands, rings, ribbed strands, star or wheel extrudates.

The catalysts can have specific surface areas of from 30 to 2000 m ² /g, preferably 100 to 700 m ² /g. The volume of the pores with a diameter of 2-20 nm is typically 0.05-0.5 ml/g, preferably 0.1 -0.3 ml/g, that of the pores of 20-200 nm is typically 0.005 to 0.2 ml/g, preferably 0.01 to 0.1 ml/g, and that of the pores of 200-2000 nm is typically 0.05-0.5 ml/g, preferably 0.05 to 0.3 ml/g. Deactivated catalysts can in most cases be regenerated by burning off in air or depleted air at 250-550 °C. Alternatively, a treatment with compounds which have an oxidizing effect at lower temperatures-optionally also in the liquid phase-is possible, in this connection mention is made in particular of NOx, H2O2 and the halogens. The regeneration can take place directly in the alkylation reactor or externally.

The alkylation can take place in the liquid phase, i.e. without gas phase, which can be achieved by a corresponding system pressure. The pressure is usually the autogenous pressure (the vapor pressure of the system) or greater. Alkylation temperatures can be 100 to 250 °C, preferably 120 to 220 °C, in particular 130 to 200 °C. Suitable pressures are in the range from 1 to 35 bar.

The alkylation may be carried out in batch or continuous mode. In the batch mode, a typical method is to use a stirred autoclave or glass flask, which may be heated to the desired reaction temperature. A continuous process is most efficiently carried out in a fixed bed process. Space rates in a fixed bed process can range from 0.01 to 10 or more weight hourly space velocity. In a fixed bed process, the alkylation catalyst is charged to the reactor and activated or dried at a temperature of at least 150°C under vacuum or flowing inert, dry gas. After activation, the alkylation catalyst is cooled to ambient temperature and a flow of the aromatic hydrocarbon compound is introduced, optionally toluene. Pressure is increased by means of a back pressure valve so that the pressure is above the bubble point pressure of the aromatic hydrocarbon feed composition at the desired reaction temperature. After pressurizing the system to the desired pressure, the temperature is increased to the desired reaction temperature. A flow of the olefin is then mixed with the aromatic hydrocarbon and allowed to flow over the catalyst. The reactor effluent comprising alkylated aromatic hydrocarbon, unreacted olefin and excess aromatic hydrocarbon compound are collected. The excess aromatic hydrocarbon compound is then removed by distillation, stripping, evaporation under vacuum, or any other means known to those skilled in the art.

The oligobutyl benzene sulfonic acid is usually produced by sulfonation of the oligobutyl benzene.

The sulfonation the oligobutyl benzene can be effected by reacting the oligobutyl benzene with a sulfonation agent, such as with concentrated sulfuric acid, with an oleum, with sulfur trioxide dilute in nitrogen or air, or with sulfur trioxide dissolved in sulfur dioxide. The sulfonation with sulfur trioxide is preferred. The sulfonation reaction can be made in stirred vessels or in a falling film reactor. After sulfonation the raw product can optionally be purified by conventional methods, such as washing with water or by thermal treatment with stirring by nitrogen bubbling.

The sulfonic acid group in the oligobutyl benzene sulfonic acid can be in the ortho, meta, or para position to the oligobutyl group, where the para position is preferred.

The sulfonate group in the oligobutyl benzene sulfonate can be in the ortho, meta, or para position to the oligobutyl group, where the para position is preferred.

The oligobutyl benzene sulfonate is usually produced by neutralizing the oligobutyl benzene sulfonic acid.

The oligobutyl benzene sulfonic acid can be neutralized using a base. Examples of suitable bases include alkali (e.g. sodium, potassium), earth alkali (e.g. calcium, magnesium), ammonium or amine (e.g., isopropylamine, methylamine, triethanolamine) salts of hydroxide, carbonate, or oxides. For instance, sodium hydroxide, potassium hydroxide, ammonium hydroxide, sodium carbonate, sodium bicarbonate, potassium carbonate, magnesium hydroxide, magnesium carbonate, basic magnesium carbonate, calcium hydroxide, and calcium carbonate, and mixtures thereof may be used for neutralization.

Following neutralization the sulfonate may be purified, e.g. by filtration, centrifuging, washing, drying, and/or other methods for removing a solid sulfonate product from aqueous solution.

The oligobutyl benzene sulfonate can have the form of a neutral or overbased alkali metal salt, earth alkali metal salt or ammonium salt.

The oligobutyl benzene sulfonate can be present in form of a salt with a cationic counterion. The oligobutyl benzene sulfonate can have the form of an alkali metal salt (e.g. lithium, sodium, potassium), earth alkali metal salt (e.g. magnesium, calcium, strontium, and barium), or ammonium salt.

In another form the oligobutyl benzene sulfonate is a calcium salt of oligobutyl benzene sulfonate, a magnesium salt of oligobutyl benzene sulfonate, or a barium salt of oligobutyl benzene sulfonate. The oligobutyl benzene sulfonate can be present as a overbased sulfonate, e.g. a low overbased sulfonate or a high overbased sulfonate.

Overbased sulfonates can be characterized by their base number (also termed BN). The BN refers to the amount of base equivalent to milligrams of KOH in one gram of sample. Thus, higher BN numbers reflect more alkaline products, and therefore a greater alkalinity reserve. The BN of a sample can be determined by ASTM Test No. D2896. A low overbased alkylaryl sulfonate often refers to an overbased sulfonate having a BN of about 2 to about 60. A high overbased alkylaryl sulfonate often refers to an overbased sulfonate having a BN of at least 250.

The overbased sulfonate can be prepared by adding a stoichiometric excess of the base (e.g. hydroxide, oxide, carbonate), based on the amount required to react with the acidic moiety of the sulfonate. Usually a diluent (e.g. a mineral oil) is incorporated in the overbased sulfonate.

In a preferred form the method for preparing the oligobutyl benzene sulfonate comprises the steps of i) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and iv) neutralizing the oligobutyl benzene sulfonic acid to produce an oligobutyl benzene sulfonate, where the alkylation catalyst for the alkylation is a zeolite, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, and where for neutralizing a base is used selected from alkali, earth alkali, ammonium or amine salts of hydroxide, carbonate, or oxides.

In a preferred form the method for preparing the oligobutyl benzene sulfonate comprises the steps of i) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and iv) neutralizing the oligobutyl benzene sulfonic acid to produce an oligobutyl benzene sulfonate, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, where the alkylation catalyst for the alkylation is a zeolite, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, and where for neutralizing a base is used selected from alkali, earth alkali, ammonium or amine salts of hydroxide, carbonate, or oxides.

In a preferred form the method for preparing the oligobutyl benzene sulfonate comprises the steps of i) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and iv) neutralizing the oligobutyl benzene sulfonic acid to produce an oligobutyl benzene sulfonate, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, where the alkene blend comprises 20 - 85 wt% of the C alkenes, 5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes, where the alkylation catalyst for the alkylation is a zeolite, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, and where for neutralizing a base is used selected from alkali, earth alkali, ammonium or amine salts of hydroxide, carbonate, or oxides.

In another preferred form the method for preparing the oligobutyl benzene sulfonate comprises the steps of i) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 700 g/mol, ii) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and iv) neutralizing the oligobutyl benzene sulfonic acid to produce an oligobutyl benzene sulfonate, where the alkylation catalyst for the alkylation is a zeolite, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, and where for neutralizing a base is used selected from alkali, earth alkali, ammonium or amine salts of hydroxide, carbonate, or oxides. In another preferred form the method for preparing the oligobutyl benzene sulfonate comprises the steps of i) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 700 g/mol, ii) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and iv) neutralizing the oligobutyl benzene sulfonic acid to produce an oligobutyl benzene sulfonate, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, where the alkylation catalyst for the alkylation is a zeolite, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, and where for neutralizing a base is used selected from alkali, earth alkali, ammonium or amine salts of hydroxide, carbonate, or oxides.

In another preferred form the method for preparing the oligobutyl benzene sulfonate comprises the steps of i) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 700 g/mol, ii) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and iv) neutralizing the oligobutyl benzene sulfonic acid to produce an oligobutyl benzene sulfonate, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, where the alkene blend comprises 20 - 85 wt% of the C alkenes, 5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes, where the alkylation catalyst for the alkylation is a zeolite, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, and where for neutralizing a base is used selected from alkali, earth alkali, ammonium or amine salts of hydroxide, carbonate, or oxides.

In another preferred form the method for preparing the oligobutyl benzene sulfonate comprises the steps of i) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 500 g/mol, ii) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and iv) neutralizing the oligobutyl benzene sulfonic acid to produce an oligobutyl benzene sulfonate, where the alkylation catalyst for the alkylation is a zeolite, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, and where for neutralizing a base is used selected from alkali, earth alkali, ammonium or amine salts of hydroxide, carbonate, or oxides.

In another preferred form the method for preparing the oligobutyl benzene sulfonate comprises the steps of v) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 500 g/mol, vi) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, vii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and viii) neutralizing the oligobutyl benzene sulfonic acid to produce an oligobutyl benzene sulfonate, where the alkylation catalyst for the alkylation is a zeolite, where the oligomerization is in the presence of a nickel containing heterogenous catalyst, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, and where for neutralizing a base is used selected from alkali, earth alkali, ammonium or amine salts of hydroxide, carbonate, or oxides.

In another preferred form the method for preparing the oligobutyl benzene sulfonate comprises the steps of i) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 500 g/mol, ii) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and iv) neutralizing the oligobutyl benzene sulfonic acid to produce an oligobutyl benzene sulfonate, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, where the alkylation catalyst for the alkylation is a zeolite, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, and where for neutralizing a base is used selected from alkali, earth alkali, ammonium or amine salts of hydroxide, carbonate, or oxides. In another preferred form the method for preparing the oligobutyl benzene sulfonate comprises the steps of i) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 500 g/mol, ii) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and iv) neutralizing the oligobutyl benzene sulfonic acid to produce an oligobutyl benzene sulfonate, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, where the alkene blend comprises 20 - 85 wt% of the C alkenes, 5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes, where the alkylation catalyst for the alkylation is a zeolite, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, and where for neutralizing a base is used selected from alkali, earth alkali, ammonium or amine salts of hydroxide, carbonate, or oxides.

In another preferred form the method for preparing the oligobutyl benzene sulfonate comprises the steps of i) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 500 g/mol, ii) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and iv) neutralizing the oligobutyl benzene sulfonic acid to produce an oligobutyl benzene sulfonate, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, where the oligomerization is in the presence of a nickel containing heterogenous catalyst, where the alkene blend comprises 20 - 85 wt% of the C alkenes, 5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes, where the alkylation catalyst for the alkylation is a zeolite, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, and where for neutralizing a base is used selected from alkali, earth alkali, ammonium or amine salts of hydroxide, carbonate, or oxides. The invention also relates to the oligobutyl benzene which is obtainable by the method for preparing the oligobutyl benzene sulfonate. The oligobutyl benzene is usually obtainable by the method for preparing the oligobutyl benzene sulfonate as intermediate.

The oligobutyl benzene is usually obtainable by the method comprising the steps of i) oligomerization of the butene mix comprising 1 -butene and 2-butene to produce the alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce the oligobutyl benzene.

The oligobutyl benzene is preferably obtainable by the method comprising the steps of i) oligomerization of the butene mix comprising 1 -butene and 2-butene to produce the alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce the oligobutyl benzene, where the oligobutenes have a molecular weight from 220 to 1000 g/mol, 220 to 700 g/mol, 220 to 500 g/mol, or 220 to 350 g/mol.

The oligobutyl benzene is preferably obtainable by the method comprising the steps of i) oligomerization of the butene mix comprising 1 -butene and 2-butene to produce the alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce the oligobutyl benzene, where the oligomerization is in the presence of a nickel containing heterogenous catalyst, and where the oligobutenes have a molecular weight from 220 to 1000 g/mol, 220 to 700 g/mol, 220 to 500 g/mol, or 220 to 350 g/mol

The oligobutyl benzene is also preferably obtainable by the method comprising the steps of i) oligomerization of the butene mix comprising 1 -butene and 2-butene to produce the alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce the oligobutyl benzene, where the oligobutenes have a molecular weight from 220 to 1000 g/mol, 220 to 700 g/mol, 220 to 500 g/mol, or 220 to 350 g/mol, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, and where the alkene blend comprises 20 - 85 wt% of the C alkenes, 5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes.

The oligobutyl benzene is also preferably obtainable by the method comprising the steps of i) oligomerization of the butene mix comprising 1 -butene and 2-butene to produce the alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce the oligobutyl benzene, where the oligobutenes have a molecular weight from 220 to 1000 g/mol, 220 to 700 g/mol, 220 to 500 g/mol, or 220 to 350 g/mol, where the oligomerization is in the presence of a nickel containing heterogenous catalyst, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, and where the alkene blend comprises 20 - 85 wt% of the C alkenes, 5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes.

The oligobutyl benzene is also preferably obtainable by the method comprising the steps of i) oligomerization of the butene mix comprising 1 -butene and 2-butene to produce the alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce the oligobutyl benzene, where the oligobutenes have a molecular weight from 220 to 1000 g/mol, 220 to 700 g/mol, 220 to 500 g/mol, or 220 to 350 g/mol, where the oligomerization is in the presence of a nickel containing heterogenous catalyst, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, and where the alkene blend comprises 20 - 85 wt% of the C alkenes, 5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes.

The invention also relates to a oligobutyl benzene sulfonic acid which is obtainable by the method for preparing the oligobutyl benzene sulfonate. The oligobutyl benzene is usually obtainable by the method for preparing the oligobutyl benzene sulfonate as intermediate.

The oligobutyl benzene sulfonic acid is usually obtainable by the method comprising the steps of i) oligomerization of the butene mix comprising 1 -butene and 2-butene to produce the alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce the oligobutyl benzene, and iii) sulfonation of the oligobutyl benzene to produce the oligobutyl benzene sulfonic acid.

The oligobutyl benzene sulfonic acid is preferably obtainable by the method comprising the steps of i) oligomerization of the butene mix comprising 1 -butene and 2-butene to produce the alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce the oligobutyl benzene, and iii) sulfonation of the oligobutyl benzene to produce the oligobutyl benzene sulfonic acid, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, where the oligobutenes have a molecular weight from 220 to 1000 g/mol, 220 to 700 g/mol, 220 to 500 g/mol, or 220 to 350 g/mol.

The oligobutyl benzene sulfonic acid is also preferably obtainable by the method comprising the steps of i) oligomerization of the butene mix comprising 1 -butene and 2-butene to produce the alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce the oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce the oligobutyl benzene sulfonic acid, where the oligomerization is in the presence of a nickel containing heterogenous catalyst, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, and where the oligobutenes have a molecular weight from 220 to 1000 g/mol, 220 to 700 g/mol, 220 to 500 g/mol, or 220 to 350 g/mol

The oligobutyl benzene sulfonic acid is also preferably obtainable by the method comprising the steps of i) oligomerization of the butene mix comprising 1 -butene and 2-butene to produce the alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce the oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce the oligobutyl benzene sulfonic acid, where the oligobutenes have a molecular weight from 220 to 1000 g/mol, 220 to 700 g/mol,

220 to 500 g/mol, or 220 to 350 g/mol, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, and where the alkene blend comprises 20 - 85 wt% of the C alkenes, 5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes.

The oligobutyl benzene sulfonic acid is also preferably obtainable by the method comprising the steps of i) oligomerization of the butene mix comprising 1 -butene and 2-butene to produce the alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce the oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce the oligobutyl benzene sulfonic acid, where the oligobutenes have a molecular weight from 220 to 1000 g/mol, 220 to 700 g/mol, 220 to 500 g/mol, or 220 to 350 g/mol, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, where the sulfonic acid group in the oligobutyl benzene sulfonic acid is in para position to the oligobutyl group, and where the alkene blend comprises 20 - 85 wt% of the C alkenes, 5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes.

The oligobutyl benzene sulfonic acid is also preferably obtainable by the method comprising the steps of i) oligomerization of the butene mix comprising 1 -butene and 2-butene to produce the alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce the oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce the oligobutyl benzene sulfonic acid, where the oligobutenes have a molecular weight from 220 to 1000 g/mol, 220 to 700 g/mol, 220 to 500 g/mol, or 220 to 350 g/mol, where the oligomerization is in the presence of a nickel containing heterogenous catalyst, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, and where the alkene blend comprises 20 - 85 wt% of the C alkenes, 5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes.

The oligobutyl benzene sulfonic acid is also preferably obtainable by the method comprising the steps of i) oligomerization of the butene mix comprising 1 -butene and 2-butene to produce the alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce the oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce the oligobutyl benzene sulfonic acid, where the oligobutenes have a molecular weight from 220 to 1000 g/mol, 220 to 700 g/mol, 220 to 500 g/mol, or 220 to 350 g/mol, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, where the oligomerization is in the presence of a nickel containing heterogenous catalyst, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, and where the alkene blend comprises 20 - 85 wt% of the C alkenes, 5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes.

The oligobutyl benzene sulfonic acid is also preferably obtainable by the method comprising the steps of i) oligomerization of the butene mix comprising 1 -butene and 2-butene to produce the alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce the oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce the oligobutyl benzene sulfonic acid, where the oligobutenes have a molecular weight from 220 to 1000 g/mol, 220 to 700 g/mol, 220 to 500 g/mol, or 220 to 350 g/mol, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, where the oligomerization is in the presence of a nickel containing heterogenous catalyst, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, where the sulfonic acid group in the oligobutyl benzene sulfonic acid is in para position to the oligobutyl group, and where the alkene blend comprises 20 - 85 wt% of the C alkenes, 5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes.

The oligobutyl benzene sulfonic acid is also preferably obtainable by the method comprising the steps of i) oligomerization of the butene mix comprising 1 -butene and 2-butene to produce the alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce the oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce the oligobutyl benzene sulfonic acid, where the oligobutenes have a molecular weight from 220 to 1000 g/mol, 220 to 700 g/mol, 220 to 500 g/mol, or 220 to 350 g/mol, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, where the oligomerization is in the presence of a nickel containing heterogenous catalyst, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, where the sulfonic acid group in the oligobutyl benzene sulfonic acid is in para position to the oligobutyl group, and where the alkene blend comprises 20 - 85 wt% of the C alkenes, 5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes.

The invention further relates to a lubricant comprising the oligobutyl benzene sulfonate. In another form the lubricant comprises the oligobutyl benzene sulfonate, which is obtainable by a method for preparing the oligobutyl benzene sulfonate comprising the steps of i) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and iv) neutralizing the oligobutyl benzene sulfonic acid to produce an oligobutyl benzene sulfonate.

In another form the lubricant comprises the oligobutyl benzene sulfonate, which is obtainable by the method for preparing the oligobutyl benzene sulfonate comprises the steps of i) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 500 g/mol, ii) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and iv) neutralizing the oligobutyl benzene sulfonic acid to produce an oligobutyl benzene sulfonate, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, where the oligomerization is in the presence of a nickel containing heterogenous catalyst, where the alkene blend comprises 20 - 85 wt% of the C alkenes, 5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes, where the alkylation catalyst for the alkylation is a zeolite, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, and where for neutralizing a base is used selected from alkali, earth alkali, ammonium or amine salts of hydroxide, carbonate, or oxides.

Typically, the lubricant comprises a base oil, the oligobutyl benzene sulfonate, and further lubricant additives.

The lubricant may comprise at least 0.1 wt%, preferably at least 0.5 wt% and in particular at least 1 wt% of the oligobutyl benzene sulfonate. In another form the lubricant may comprise 0.1 - 20 wt%, preferably 0.1 - 150 wt% and in particular at least 0.1 - 10 wt% of the oligobutyl benzene sulfonate.

The lubricant may comprise at least 30 wt%, preferably at least 50 wt% and in particular at least 70 wt% of the base oil. The lubricant may comprise 30 - 99.9 wt%, preferably 50 - 99 wt% and in particular 70 - 95 wt% of the base oil.

The lubricant may comprise up to 20 wt%, preferably up to 15 wt% and in particular up to 10 wt% of the further lubricant additive.

Lubricants usually refers to composition which are capable of reducing friction between surfaces (preferably metal surfaces), such as surfaces of mechanical devices. A mechanical device may be a mechanism consisting of a device that works on mechanical principles. Suitable mechanical device are bearings, gears, joints and guidances. The mechanical device may be operated at temperatures in the range of -30 C to 80 °C.

The lubricant is usually a lubricating liquid, lubricating oil or lubricating grease. Lubricants are usually specifically formulated for virtually every type of machine and manufacturing process. The type and concentration of base oils and/or lubricant additives used for these lubricants may be selected based on the requirements of the machinery or process being lubricated, the quality required by the builders and the users of the machinery, and the government regulation. Typically, each lubricant has a unique set of performance requirements. In addition to proper lubrication of the machine or process, these requirements may include maintenance of the quality of the lubricant itself, as well as the effect of the lubricant’ s use and disposal on energy use, the quality of the environment, and on the health of the user.

Typical lubricants are automotive lubricants (e.g. gasoline engine oils, diesel engine oils, gas engine oils, gas turbine oils, automatic transmission fluids, gear oils) and industrial lubricants (e.g. industrial gear oils, pneumatic tool lubricating oil, high temperature oil, gas compressor oil, hydraulic fluids, metalworking fluids).

Examples for lubricants are axel lubrication, medium and heavy duty engine oils, industrial engine oils, marine engine oils, automotive engine oils, crankshaft oils, compressor oils, refrigerator oils, hydrocarbon compressor oils, very low-temperature lubricating oils and fats, high temperature lubricating oils and fats, wire rope lubricants, textile machine oils, refrigerator oils, aviation and aerospace lubricants, aviation turbine oils, transmission oils, gas turbine oils, spindle oils, spin oils, traction fluids, transmission oils, plastic transmission oils, passenger car transmission oils, truck transmission oils, industrial transmission oils, industrial gear oils, insulating oils, instrument oils, brake fluids, transmission liquids, shock absorber oils, heat distribution medium oils, transformer oils, fats, chain oils, minimum quantity lubricants for metalworking operations, oil to the warm and cold working, oil for water-based metalworking liquids, oil for neat oil metalworking fluids, oil for semi-synthetic metalworking fluids, oil for synthetic metalworking fluids, drilling detergents for the soil exploration, hydraulic oils, in biodegradable lubricants or lubricating greases or waxes, chain saw oils, release agents, molding fluids, gun, pistol and rifle lubricants or watch lubricants and food grade approved lubricants.

The lubricant has usually may have a kinematic viscosity at 40 °CC of at least 10, 50, 100, 150, 200, 300, 400, 500, 600, 900, 1400, or 2000 mm ² /s. In another form the lubricant has usually may have a kinematic viscosity at 40 °C from 200 to 30 000 mm ² /s (cSt), preferably from 500 to 10 000 mm ² /s, and in particular from 1000 to 5000 mm ² /s. The lubricant has usually may have a kinematic viscosity at 100 °C of at least 2, 3, 5, 10, 20, 30, 40, or 50 mm ² /s. In another form the lubricant may have a kinematic viscosity at 100 °C from 10 to 5000 mm ² /s (cSt), preferably from 30 to 3000 mm ² /s, and in particular from 50 to 2000 mm ² /s

The lubricant may have a viscosity index (VI) of at least 150, 160, 170, 180, 190 or 200.

The base oil may selected from the group consisting of mineral oils (Group I, II or III oils), polyalphaolefins (Group IV oils), polymerized and interpolymerized olefins, alkyl naphthalenes, alkylene oxide polymers, silicone oils, phosphate esters and carboxylic acid esters (Group V oils). Preferably, the base oil is selected from Group I, Group II, Group III base oils according to the definition of the API, or mixtures thereof. Definitions for the base oils are the same as those found in the American Petroleum Institute (API) publication "Engine Oil Licensing and Certification System", Industry Services Department, Fourteenth Edition, December 1996, Addendum 1, December 1998. Said publication categorizes base oils as follows: a) Group I base oils contain less than 90 percent saturates (ASTM D 2007) and/or greater than 0.03 percent sulfur (ASTM D 2622) and have a viscosity index (ASTM D 2270) greater than or equal to 80 and less than 120. b) Group II base oils contain greater than or equal to 90 percent saturates and less than or equal to 0.03 percent sulfur and have a viscosity index greater than or equal to 80 and less than 120. c) Group III base oils contain greater than or equal to 90 percent saturates and less than or equal to 0.03 percent sulfur and have a viscosity index greater than or equal to 120. d) Group IV base oils contain polyalphaolefins. Polyalphaolefins (PAG) include known PAO materials which typically comprise relatively low molecular weight hydrogenated polymers or oligomers of alphaolefins which include but are not limited to C2 to about C32 alphaole-fins with the C8 to about C16 alphaolefins, such as 1 -octene, 1 -decene, 1 -dodecene and the like being preferred. The preferred polyalphaolefins are poly-1 - octene, poly-1 -decene, and poly-1 -dode-cene. e) Group V base oils contain any base oils not described by Groups I to IV. Examples of Group V base oils include alkyl naphthalenes, alkylene oxide polymers, silicone oils, and phosphate esters.

Synthetic base oils include hydrocarbon oils and halo-substituted hydrocarbon oils such as polymerized and interpolymerized olefins (e.g., polypropylenes, propylene-isobutylene copolymers, chlorinated polybutylenes, poly(1 -hexenes), poly(1 -octenes), poly(1 -decenes)); alkylbenzenes (e.g., dodecylbenzenes, tetradecylbenzenes, dinonylbenzenes, di(2- ethylhexyl)benzenes); poly-phenyls (e.g., biphenyls, terphenyls, alkylated polyphenols); and alkylated diphenyl ethers and alkylated diphenyl sulfides and derivative, analogs and homologs thereof.

Alkylene oxide polymers and interpolymers and derivatives thereof where the terminal hydroxyl groups have been modified by esterification, etherification, etc., constitute another class of known synthetic base oils. These are exemplified by polyoxyalkylene polymers prepared by polymeriza-tion of ethylene oxide or propylene oxide, and the alkyl and aryl ethers of polyoxyalkylene poly-mers (e.g., methyl-polyisopropylene glycol ether having a molecular weight of 1000 or diphenyl ether of polyethylene glycol having a molecular weight of 1000 to 1500); and mono- and polycar-boxylic esters thereof, for example, the acetic acid esters, mixed C3-C8 fatty acid esters and C13 oxo acid diester of tetraethylene glycol.

Silicon-based oils such as the polyalkyl-, polyaryl-, polyalkoxy- or polyaryloxysilicone oils and sili-cate oils comprise another useful class of synthetic base oils; such base oils include tetraethyl silicate, tetraisopropyl silicate, tetra-(2- ethylhexyl)silicate, tetra-(4-methyl-2- ethylhe-xyl) silicate, tetra-(p-tert-butyl-phenyl) silicate, hexa-(4-methyl-2- ethylhexyl)disiloxane, poly(methyl) siloxanes and poly(methylphenyl)siloxanes. Other synthetic base oils include liquid esters of phosphorous-containing acids (e.g., tricresyl phosphate, trioctyl phosphate, diethyl ester of decylphosphonic acid) and polymeric tetrahydrofurans.

The lubricant may further comprise a lubricant additive. Suitable lubricant additives may be selected from viscosity index improvers, polymeric thickeners, corrosion inhibitors, detergents, dispersants, anti-foam agents, dyes, wear protection additives, extreme pressure additives (EP additives), anti-wear additives (AW additives), friction modifiers, metal deactivators, pour point depressants.

The total combined amount of the lubricant additive in the lubricant may include ranges of CI- 25 wt%, or 0.01-20 wt%, or 0.1-15 wt% or 0.5-10 wt%, or 1-5 wt% of the lubricant.

The viscosity index improvers include high molecular weight polymers that increase the relative viscosity of an oil at high temperatures more than they do at low temperatures. Viscosity index improvers include polyacrylates, polymethacrylates, alkylmethacrylates, vinylpyrrolidone/meth-acrylate copolymers, poly vinylpyrrolidones, polybutenes, olefin copolymers such as an ethylene-propylene copolymer or a styrene-butadiene copolymer or polyalkene such as PI B, styrene/acrylate copolymers and polyethers, and combinations thereof. The most common VI improvers are methacrylate polymers and copolymers, acrylate polymers, olefin polymers and copolymers, and styrenebutadiene copolymers. Other examples of the viscosity index improver include polymethacrylate, polyisobutylene, alpha-olefin polymers, alpha-olefin copolymers (e.g., an ethylenepropylene copolymer), polyalkylstyrene, phenol condensates, naphthalene condensates, a styrenebutadiene copolymer and the like. Of these, polymethacrylate having a number average molecular weight of 10000 to 300000, and alpha-olefin polymers or alpha-olefin copolymers having a number average molecular weight of 1000 to 30000, particularly ethylene- alpha-olefin copolymers having a number average molecular weight of 1000 to 10000 are preferred. The viscosity index increasing agents can be added and used individually or in the form of mixtures, conveniently in an amount within the range of from > 0.05 to < 20.0 % by weight, in relation to the weight of the base stock.

Suitable (polymeric) thickeners include, but are not limited to, polyisobutenes (PIB), oligomeric co-polymers (OCPs), polymethacrylates (PMAs), copolymers of styrene and butadiene, or high viscosity esters (complex esters).

Corrosion inhibitors may include various oxygen-, nitrogen-, sulfur-, and phosphorus- containing materials, and may include metal-containing compounds (salts, organometallics, etc.) and nonmetal-containing or ashless materials. Corrosion inhibitors may include, but are not limited to, additive types such as, for example, hydrocarbyl-, aryl-, alkyl-, arylalkyl-, and alkylaryl versions of detergents (neutral, overbased), sulfonates, phenates, salicylates, alcoholates, carboxylates, salixarates, phosphites, phosphates, thiophosphates, amines, amine salts, amine phosphoric acid salts, amine sulfonic acid salts, alkoxylated amines, etheramines, polyetheramines, amides, imides, azoles, diazoles, triazoles, benzotriazoles, benzothiadoles, mercaptobenzothiazoles, tolyltriazoles (TTZ-type), heterocyclic amines, heterocyclic sulfides, thiazoles, thiadiazoles, mercaptothiadiazoles, dimercaptothiadiazoles (DMTD-type), imidazoles, benzimidazoles, dithiobenzimidazoles, imidazolines, oxazolines, Mannich reactions products, glycidyl ethers, anhydrides, carbamates, thiocarbamates, dithiocarbamates, polyglycols, etc., or mixtures thereof.

Detergents include cleaning agents that adhere to dirt particles, preventing them from attaching to critical surfaces. Detergents may also adhere to the metal surface itself to keep it clean and prevent corrosion from occurring. Detergents include calcium alkylsalicylates, calcium alkylphenates and calcium alkarylsulfonates with alternate metal ions used such as magnesium, barium, or sodium. Examples of the cleaning and dispersing agents which can be used include metal-based detergents such as the neutral and basic alkaline earth metal sulphonates, alkaline earth metal phenates and alkaline earth metal salicylates alkenylsuccinimide and alkenylsuccinimide esters and their borohydrides, phenates, salienius complex detergents and ashless dispersing agents which have been modified with sulphur compounds. These agents can be added and used individually or in the form of mixtures, conveniently in an amount within the range of from > 0.01 to < 1.0 % by weight in relation to the weight of the base stock; these can also be high total base number (TBN), low TBN, or mixtures of high/low TBN.

Dispersants are lubricant additives that help to prevent sludge, varnish and other deposits from forming on critical surfaces. The dispersant may be a succinimide dispersant (for example N-substituted long chain alkenyl succinimides), a Mannich dispersant, an ester- containing dispersant, a condensation product of a fatty hydrocarbyl monocarboxylic acylating agent with an amine or ammonia, an alkyl amino phenol dispersant, a hydrocarbyl- amine dispersant, a polyether dispersant or a polyetheramine dispersant. In one embodiment, the succinimide dispersant includes a polyisobutylene-substituted succinimide, wherein the polyisobutylene from which the dispersant is derived may have a number average molecular weight of about 400 to about 5000, or of about 950 to about 1600. In one embodiment, the dispersant includes a borated dispersant. Typically, the borated dispersant includes a succinimide dispersant including a polyisobutylene succinimide, wherein the polyisobutylene from which the dispersant is derived may have a number average molecular weight of about 400 to about 5000. Borated dispersants are described in more detail above within the extreme pressure agent description.

Anti-foam agents may be selected from silicones, polyacrylates, and the like. The amount of anti-foam agent in the lubricant compositions described herein may range from > 0.001 wt.-% to< 0.1 wt.-% based on the total weight of the formulation. As a further example, an anti-foam agent may be present in an amount from about 0.004 wt.-% to about 0.008 wt.-%.

Suitable extreme pressure agent is a sulfurcontaining compound. In one embodiment, the sulfur-containing compound may be a sulfurised olefin, a polysulfide, or mixtures thereof. Examples of the sulfurised olefin include a sulfurised olefin derived from propylene, isobutylene, pentene; an organic sulfide and/or polysulfide including benzyldisulfide; bis- (chlorobenzyl) disulfide; dibutyl tetrasulfide; di-tertiary butyl polysulfide; and sulfurised methyl ester of oleic acid, a sulfurised alkylphenol, a sulfurised dipentene, a sulfurised terpene, a sulfurised Diels-Alder adduct, an alkyl sulphenyl N'N dialkyl dithiocarbamates; or mixtures thereof. In one embodiment, the sulfurised olefin includes a sulfurised olefin derived from propylene, isobutylene, pentene or mixtures thereof. In one embodiment the extreme pressure additive sulfur-containing compound includes a dimercaptothiadiazole or derivative, or mixtures thereof. Examples of the dimercaptothiadiazole include compounds such as 2,5- dimercapto-1 ,3,4-thiadiazole or a hydrocarbyl-substituted 2,5-dimercapto-1,3,4-thiadiazole, or oligomers thereof. The oligomers of hydrocarbyl-substituted 2, 5-di mercapto- 1 ,3,4- thiadiazole typically form by forming a sulfur-sulfur bond between 2,5-dimercapto-1,3,4- thiadiazole units to form derivatives or oligomers of two or more of said thiadiazole units. Suitable 2,5-dimercapto-1,3,4-thiadiazole derived compounds include for example 2,5- bis(tert-nonyldithio)- 1 ,3,4-thiadiazole or 2-tert-nonyldithio-5-mercapto-1 ,3,4-thiadiazole. The number of carbon atoms on the hydrocarbyl substituents of the hydrocarbyl-substituted 2,5- dimercapto-1 ,3,4-thiadiazole typically include 1 to 30, or 2 to 20, or 3 to 16. Extreme pressure additives include compounds containing boron and/or sulfur and/or phosphorus. The extreme pressure agent may be present in the lubricant compositions at 0 wt.-% to about 20 wt.-%, or at about 0.05 wt.-% to about 10.0 wt.-%, or at about 0.1 wt.-% to about 8 wt.-% of the lubricant composition.

Examples of anti-wear additives include organo borates, organo phosphites such as didodecyl phosphite, organic sulfur-containing compounds such as sulfurized sperm oil or sulfurized terpenes, zinc dialkyl dithiophosphates, zinc diaryl dithiophosphates, phosphosulfurized hydrocarbons and any combinations thereof.

Friction modifiers may include metal-containing compounds or materials as well as ashless compounds or materials, or mixtures thereof. Metal-containing friction modifiers include metal salts or metalligand complexes where the metals may include alkali, alkaline earth, or transition group metals. Such metal-containing friction modifiers may also have lowash characteristics. Transition metals may include Mo, Sb, Sn, Fe, Cu, Zn, and others. Ligands may include hydrocarbyl derivative of alcohols, polyols, glycerols, partial ester glycerols, thiols, carboxylates, carbamates, thiocarbamates, dithiocarbamates, phosphates, thiophosphates, dithiophosphates, amides, imides, amines, thiazoles, thiadiazoles, dithiazoles, diazoles, triazoles, and other polar molecular functional groups containing effective amounts of O, N, S, or P, individually or in combination. In particular, Mo-containing compounds can be particularly effective such as for example Mo-dithiocarbamates, Mo(DTC), Mo-dithiophosphates, Mo(DTP), Mo-amines, Mo (Am), Mo-alcoholates, Mo alcohol-amides, and the like.

Ashless friction modifiers may also include lubricant materials that contain effective amounts of polar groups, for example, hydroxyl-containing hydrocarbyl base oils, glycerides, partial glycerides, glyceride derivatives, and the like. Polar groups in friction modifiers may include hydrocarbyl groups containing effective amounts of O, N, S, or P, individually or in combination. Other friction modifiers that may be particularly effective include, for example, salts (both ash-containing and ashless derivatives) of fatty acids, fatty alcohols, fatty amides, fatty esters, hydroxyl-containing carboxylates, and comparable synthetic long-chain hydrocarbyl acids, alcohols, amides, esters, hydroxy carboxylates, and the like. In some instances, fatty organic acids, fatty amines, and sulfurized fatty acids may be used as suitable friction modifiers. Examples of friction modifiers include fatty acid esters and amides, organo molybdenum compounds, molybdenum dialkylthiocarbamates and molybdenum dialkyl dithiophosphates.

Suitable metal deactivators include benzotriazoles and derivatives thereof, for example 4- or 5-alkylbenzotriazoles (e.g. triazole) and derivatives thereof, 4, 5,6,7- tetrahydrobenzotriazole and 5,5'-methylenebisbenzotriazole; Mannich bases of benzotriazole or triazole, e.g. 1-[bis(2-ethyl-hexyl) aminomethyl) triazole and 1-[bis(2- ethylhexyl) aminomethyl)benzotriazole; and alkoxy-alkyl benzotriazoles such as 1- (nonyloxymethyl)benzotriazole, 1-(1 -butoxyethyl) benzotriazole and 1-(1 -cyclohexyloxybutyl) triazole, and combinations thereof. Additional non-limiting examples of the one or more metal deactivators include 1 ,2,4-triazoles and derivatives thereof, for example 3-alkyl(or aryl)- 1 , 2,4-triazoles, and Mannich bases of 1,2,4-triazoles, such as 1-[bis(2-ethylhexyl) aminomethyl -1, 2,4-triazole; alkoxyalky1-1, 2,4-triazoles such as 1-(1-bu-toxyethyl)-1, 2,4- triazole; and acylated 3-amino-1, 2,4-triazoles, imidazole derivatives, for example 4,4'- methylenebis(2-undecyl-5-methylimidazole) and bis[(N-methyl)imidazol-2-yl]-carbinol octyl ether, and combinations thereof. Further non-limiting examples of the one or more metal deactivators include sulfur-containing heterocyclic compounds, for example 2-mercapto- benzothiazole, 2,5-dimercapto-1, 3,4-thia-diazole and derivatives thereof; and 3,5-bis[di(2- ethylhexyl) aminomethyl]-1, 3,4-thiadiazolin-2-one, and combinations thereof. Even further non-limiting examples of the one or more metal deactivators include amino compounds, for example salicylidenepropylenediamine, salicylami-noguanidine and salts thereof, and combinations thereof. The one or more metal deactivators are not particularly limited in amount in the composition but are typically present in an amount of from about 0.01 to about 0.1 , from about 0.05 to about 0.01 , or from about 0.07 to about 0.1 , wt.-% based on the weight of the composition. Alternatively, the one or more metal deactivators may be present in amounts of less than about 0.1 , of less than about 0.7, or less than about 0.5, wt.-% based on the weight of the composition. Pour point depressants (PPD) include polymethacrylates, alkylated naphthalene derivatives, and combinations thereof. Commonly used additives such as alkylaromatic polymers and polymethacrylates are also useful for this purpose. Typically, the treat rates range from > 0.001 wt.-% to < 1.0 wt.-%, in relation to the weight of the base stock.

Demulsifiers include trialkyl phosphates, and various polymers and copolymers of ethylene glycol, ethylene oxide, propylene oxide, or mixtures thereof.

The invention also relates to a fuel comprising the oligobutyl benzene sulfonate. In another form the fuel comprises the oligobutyl benzene sulfonate, which is obtainable by a method for preparing the oligobutyl benzene sulfonate comprising the steps of i) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 2000 g/mol, ii) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and iv) neutralizing the oligobutyl benzene sulfonic acid to produce an oligobutyl benzene sulfonate.

In another form the fuel comprises the oligobutyl benzene sulfonate, which is obtainable by the method for preparing the oligobutyl benzene sulfonate comprises the steps of i) oligomerization of a butene mix comprising 1 -butene and 2-butene to produce an alkene blend which comprises oligobutenes with a molecular weight of 220 to 500 g/mol, ii) alkylation of benzene with the alkene blend to produce an oligobutyl benzene, iii) sulfonation of the oligobutyl benzene to produce a oligobutyl benzene sulfonic acid, and iv) neutralizing the oligobutyl benzene sulfonic acid to produce an oligobutyl benzene sulfonate, where the butene mix contains from 50 to 99 wt%, based on the total olefin content, of 1- butene and 2-butene, where the oligomerization is in the presence of a nickel containing heterogenous catalyst, where the alkene blend comprises 20 - 85 wt% of the C alkenes, 5 - 30 wt% of the C20 alkenes, and 2 - 20 wt% of the C24 alkenes, where the alkylation catalyst for the alkylation is a zeolite, where the sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide, and where for neutralizing a base is used selected from alkali, earth alkali, ammonium or amine salts of hydroxide, carbonate, or oxides. The fuel may comprise at least 1 mg/kg, preferably at least 10 mg/kg and in particular at least 50 mg/kg of the oligobutyl benzene sulfonate.

In another form the fuel (such as automotive fuels for cars or trucks) may comprise 1 mg/kg - 1000 mg/kg, preferably 10 mg/kg - 500 mg/kg and in particular at least 50 - 200 mg/kg of the oligobutyl benzene sulfonate.

In another form (such as for marine fuel or aviation fuel) the fuel may comprise 0.001 - 10 wt%, preferably 0.001 - 5 wt% and in particular at least 0.01 - 2.5 wt% of the oligobutyl benzene sulfonate.

The fuel can be understood to mean middle distillate fuels of fossil, vegetable or animal origin, biofuel ("biodiesel") and mixtures of such middle distillate fuels and biofuels.

Middle distillate fuels (also called "middle distillates" for short hereinafter) are especially understood to mean fuels which are obtained by distilling crude oil as the first process step and boil within the range from 120 to 450°C. Such middle distillate fuels are used especially as diesel fuel, heating oil or kerosene, particular preference being given to diesel fuel and heating oil. Preference is given to using low-sulfur middle distillates, i.e. those which comprise less than 350 ppm of sulfur, especially less than 200 ppm of sulfur, in particular less than 50 ppm of sulfur. In special cases they comprise less than 10 ppm of sulfur; these middle distillates are also referred to as "sulfur-free". They are generally crude oil distillates which have been subjected to refining under hydrogenating conditions and therefore comprise only small proportions of polyaromatic and polar compounds. They are preferably those middle distillates which have 90% distillation points below 370°C, especially below 360°C and in special cases below 330°C.

Low-sulfur and sulfur-free middle distillates may also be obtained from relatively heavy mineral oil fractions which cannot be distilled under atmospheric pressure. Typical conversion processes for preparing middle distillates from heavy crude oil fractions include: hydrocracking, thermal cracking, catalytic cracking, coking processes and/or visbreaking. Depending on the process, these middle distillates are obtained in low-sulfur or sulfur-free form, or are subjected to refining under hydrogenating conditions. The middle distillates preferably have aromatics contents of below 28% by weight, especially below 20% by weight. The content of normal paraffins is between 5% by weight and 50% by weight, preferably between 10 and 35% by weight. In the context of the present invention, middle distillate fuels shall also be understood here to mean those fuels which can either be derived indirectly from fossil sources such as mineral oil or natural gas, or else are produced from biomass via gasification and subsequent hydrogenation. A typical example of a middle distillate fuel which is derived indirectly from fossil sources is the GTL ("gas-to-liquid") diesel fuel obtained by means of Fischer-Tropsch synthesis. A middle distillate is prepared from biomass, for example, via the BTL ("biomass- to-liquid") process, and can be used as fuel either alone or in a mixture with other middle distillates. The middle distillates also include hydrocarbons which are obtained by the hydrogenation of fats and fatty oils. They comprise predominantly n-paraffins.

In a preferred embodiment the fuel is a diesel fuel (absent any additives) with a CP value according to ASTM D2500/ASTM D97 of 0 to -15 °C, preferably 0 to -10 °C, and more preferably -5 to -10 °C and/or, preferably and with a content of n-paraffines of from 10 to 27 % by weight, more preferably of from 15 to 25 % by weight, and most preferably from 17 to 23 % by weight.

In addition to its use in the middle distillate fuels of fossil, vegetable or animal origin mentioned, which are essentially hydrocarbon mixtures, the inventive copolymer can also be used in biofuel oils and in mixtures of the middle distillates mentioned with biofuel oils, in order to improve cold flow characteristics. Mixtures of this kind are commercially available and usually comprise the biofuel oils in minor amounts, typically in amounts of 1% to 30% by weight, especially of 3% to 10% by weight, based on the total amount of middle distillate of fossil, vegetable or animal origin and biofuel oil.

Biofuel are generally based on fatty acid esters, preferably essentially on alkyl esters of fatty acids which derive from vegetable and/or animal oils and/or fats. Alkyl esters are preferably understood to mean lower alkyl esters, especially Ci- to C4-alkyl esters, which are obtainable by transesterifying the glycerides which occur in vegetable and/or animal oils and/or fats, especially triglycerides, by means of lower alcohols, for example ethanol or in particular methanol ("FAME"). Typical lower alkyl esters which are based on vegetable and/or animal oils and/or fats and find use as a biofuel oil or components thereof are, for example, HVO (hydrogenated vegetable oil), sunflower methyl ester, palm oil methyl ester ("PME"), soya oil methyl ester ("SME") and especially rapeseed oil methyl ester ("RME").

The fuel may be a marine fuel, such as MGO (Marine gas oil), MDO (Marine diesel oil), IFO (Intermediate fuel oil), MFO (Marine fuel oil), or HFO (Heavy fuel oil). Further examples for marine fuel are IFO 380 (an Intermediate fuel oil with a maximum viscosity of 380 centistokes (<3.5% sulphur)), IFO 180 (an Intermediate fuel oil with a maximum viscosity of 180 centistokes (<3.5% sulphur)), LS 380 (a Low-sulphur (<1.0%) intermediate fuel oil with a maximum viscosity of 380 centistokes), LS 180 (a Low-sulphur (<1.0%) intermediate fuel oil with a maximum viscosity of 180 centistokes), LSMGO (a Low-sulphur (<0.1%) Marine Gas Oil, which is to often be used in European Ports and Anchorages according to EU Sulphur directive 2005/33/EC), or ULSMGO (a Ultra-Low-Sulphur Marine Gas Oil, also referred to as Ultra-Low-Sulfur Diesel (sulphur 0.0015% max). Further suitable marine fuels are according to DIN ISO 8217 of the category ISO-F- DMX, DMA, DFA, DMZ, DFZ, or DFB, or ISO-F RMA, RMB, RMD, RME, RMG, or RMK. Further suitable marine fuel is distillate marine diesel or residual marine diesel.

The fuel may comprise further additives, such as carrier oils, cold flow improvers, lubricity improvers, corrosion inhibitors, dehazers, antifoams, cetane number improvers, combustion improvers, antioxidants or stabilizers, antistats, metallocenes, metal deactivators, and/or dyes.

The invention also relates to a use of the oligobutyl benzene sulfonate as lubricant additive or fuel additive. The oligobutyl benzene sulfonate can be added to the lubricants or the fuels, e.g. for improving their performance.

The lubricant additive can comprise 1 - 80 wt%, preferably 5 - 50 wt% and in particular at least 20 - 70 wt% of the oligobutyl benzene sulfonate. The lubricant additive can comprise further lubricant additives or a base oil, e.g. a mineral oil.

The fuel additive can comprise 1 - 80 wt%, preferably 5 - 50 wt% and in particular at least 20 - 70 wt% of the oligobutyl benzene sulfonate. The fuel additive can comprise further lubricant additives or a base oil, e.g. a mineral oil.

Examples

Example 1 -Oligomerization of butene mix

An alkene blend is prepared starting from a butene mix which is obtained from a raffinate II stream. The butene mix comprises about isobutane: 3% by weight n-butane: 15% by weight isobutene: 2% by weight

1 -butene: 30% by weight trans-2-butene: 32% by weight cis-2-butene: 18% by weight.

The butene mix is oligomerized in the presence of a nickel containing heterogenous catalyst in an isothermally operated reactor having a length of about 1.5 m and a diameter of 30 mm at 20 bar and 80 °C.

The nickel containing heterogenous catalyst is a material which is produced as described in WO1 995/14647 in the form of pellets (5 mm x 5 mm). The composition in % by weight of the active components is typically: 50% by weight of NiO, 12.5% by weight of TiC>2, 33.5% by weight of SiC>2, 4% by weight of AI2O3.

The throughput is 0.75 kg of raffinate ll/(l (cat) x h). The reaction is carried out without recirculation of C4-hydrocarbons. The C4 conversion, based on the butenes comprised in the raffinate II is about 52.0% by weight. The selectivity in % by weight in the alkene blend is as follows: Cs alkenes: 76.9; C12 alkenes: 18.4 and C and higher alkenes: 4.7.

2.0 kg of this alkene blend are subjected to fractionation over an 80 cm packed column (wiremesh coils) with a reflux ratio of 1 :5 to yield:

- 1 ,45 kg Fraction A (comprising mainly Cs alkenes) with boiling interval 100-130 °C at 950 mbar

- 0,35 kg Fraction B (comprising mainly C12 alkenes) with boiling interval 100-130 °C at 950 mbar

- 0,18 kg Fraction C (comprising mainly G and higher alkenes) in the distillation bottom. According to GC analysis, Fraction C consists of 7% C12 alkenes, 70% C alkenes, 17% C20 alkenes, and 6% C24 and higher alkenes.

Example 2 -Alkylation of benzene with Fraction C alkene blend

An oligobutyl benzene is prepared starting from benzene and Fraction C of Example 1 , which contains the following oligobutenes:

7% C12 alkenes

70% C alkenes

17% C20 alkenes, and

6% C24 and higher alkenes.

The alkylation catalyst is a zeolite and the Friedel-Crafts alkylation is successfully made to produce the corresponding oligobutyl benzene. Example 3 -Alkylation of benzene with alkene blend of Fraction B and C

An oligobutyl benzene is prepared starting from benzene and a mixture of Fraction B and Fraction C of Example 1, which contains the following oligobutenes:

38% C12 alkenes

43% Cie alkenes

13% C20 alkenes, and

6% C24 and higher alkenes.

The alkylation catalyst is a zeolite and the Friedel-Crafts alkylation is successfully made to produce the corresponding oligobutyl benzene.

Example 4 -Sulfonation of oligobutylbenzene of Example 2

An oligobutyl benzene sulfonic acid is prepared by sulfonation of the oligobutyl benzene from Example 2. The sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide. The sulfonic acid group is mainly in para position to the oligobutyl group, which can be determined by H-NMR.

Example 5 -Sulfonation of oligobutylbenzene of Example 3

An oligobutyl benzene sulfonic acid is prepared by sulfonation of the oligobutyl benzene from Example 2. The sulfonation is effected by reacting the oligobutyl benzene with sulfur trioxide. The sulfonic acid group is mainly in para position to the oligobutyl group, which can be determined by H-NMR.

Example 6 - Sulfonates by Neutralization

The oligobutyl benzene sulfonic acid from Example 4 is neutralized with eguimolar amounts of

- calcium hydroxide to yield oligobutyl benzene sulfonate calcium salt.

- magnesium carbonate to yield oligobutyl benzene sulfonate magnesium salt.

To make overbased sulfonates the oligobutyl benzene sulfonic acid from Example 4 is is neutralized with a molar excess of

- calcium hydroxide to yield overbased oligobutyl benzene sulfonate calcium salt.

- magnesium carbonate to yield overbased oligobutyl benzene sulfonate magnesium salt.

Example 7 - Sulfonates by Neutralization

The oligobutyl benzene sulfonic acid from Example 5 is neutralized with eguimolar amounts of calcium hydroxide to yield oligobutyl benzene sulfonate calcium salt. magnesium carbonate to yield oligobutyl benzene sulfonate magnesium salt. To make overbased sulfonates the oligobutyl benzene sulfonic acid from Example 5 is is neutralized with a molar excess of

- calcium hydroxide to yield overbased oligobutyl benzene sulfonate calcium salt.

- magnesium carbonate to yield overbased oligobutyl benzene sulfonate magnesium salt.