Alkyl benzene sulfonic acids and corresponding salts for enhanced oil recovery

Abstract

The present invention is directed to a composition comprising isomers of alkyl benzene sulfonates, wherein the composition comprises the structural isomers ABS(I) and ABS(II) in a molar ratio ABS(I) : ABS(II) ranging from 10:90 to 30:70, and wherein the composition comprises at least one further alkyl benzene sulfonate selected from ABS(III), ABS(IV) and ABS(V). The present invention is furthermore directed to a manufacturing method of these compositions and the use of these compositions in oilfield and enhanced oil recovery applications.

Description

Alkyl benzene sulfonic acids and corresponding salts for enhanced oil recovery Background of the inventionIn industrialized economies crude oil has been the most important source of energy and starting material for numerous products of chemical industry since the early decades of the 20th century. It is commonly produced from subterranean deposits that formed over millions of years. Therefore, global stocks are limited, and it is generally accepted that deposits will be depleted within the forthcoming decades. In view of this, it is generally desired to maximize the amount of oil recovered from developed deposits. The recovery of oil from subterranean deposits can be generally divided into the phase of primary, secondary and tertiary recovery. Primary recovery relates to the phase of oil production during which oil can be extracted from a subterranean deposit by means of the natural pressure of the deposit which pushes oil from the deposit to the surface through a drilled well. Primary recovery usually allows theextraction of about 5 to 10 % of the oil in the deposit. When the natural pressure of the deposit is exhausted and further extraction by means of primary recovery is not possible or if the pressure naturally present in the deposit is not sufficient for extraction of oil, secondary recovery is usually employed, i.e. pressurized water or gas is injected into the deposit to drive oil remaining after the phase of primary recovery from the deposit. This is achieved by so-called voidage replacement, i.e. the increase and / or re-establishing of natural pressure that was present when extraction of oil was begun, as well as by sweeping or displacing oil from the deposit such that it is pushed towards a well through which it is transported to the surface. If the material injected into the deposit is water the technique is also referred to as water-flooding. Secondary recovery usually allows the extraction of additional 20 to 30 % of the oil in the deposit. Tertiary recovery relates, among others, to the phase of oil production during which chemicals such as polymers, alkaline agents, surfactants, or combinations of such chemicals are injected into the deposit in order to improve the flow of the oil remaining after primary and secondary recovery phases. This is also referred to as chemical flooding or chemical enhanced oil recovery (commonly abbreviated as EOR). Tertiary recovery usually allows the extraction of additional 10 to 20 % of the oil in the deposit. Injection of surfactants into the deposit lower the interfacial tension between oil and water and / or the sediment of the deposit. Thus, the displacement of oil droplets through the deposit is enhanced.  Alkylbenzene sulfonates are currently one of the well-known surfactants, finding use in a variety of applications where surfactants are required (detergents, hard-surface cleaners, drilling fluids, cutting fluids, wetting agent, emulsifier for agricultural herbicides, emulsion polymerization, etc.) and they have been recognized as promising for enhanced oil recovery by surfactant flooding and surfactant-polymer flooding. The main difference between alkylbenzene sulfonates used for household detergents and EOR application will be discussed later in this introduction. Alkylbenzene sulfonates are typically formed through the alkylation of benzene with olefins or with partially dehydrogenated paraffins to form a linear alkylbenzene (LAB), which comprises a hydrocarbyl radical attached to a benzene ring. The LAB is then subjected to sulfonation, in which a sulfonate group is chemically bonded to a carbon atom in the benzene ring structure of the LAB. The resulting linear alkylbenzene sulfonate (LAS) therefore contains a hydrophilic sulfonate group and a hydrophobic hydrocarbyl portion. Alkylation and sulfonation processes useful for forming LAB and LAS compositions are well known. See, e.g., U.S. Pat. No. 6,887,839. LAS are generally used in EOR applications not only because they are able to lower the interfacial tension between oil and water, but also because when used in conjunction with varying amounts of other salts, such as, sodium chloride they exhibit desirable phase behavior. The crude oil in the deposit will form a microemulsion with a well-tailored EOR compositions comprising LAS (optimum phase behavior match), the high volumes of oil and water solubilized in the microemulsion result in ultra-low interfacial tensions that provide potential for high oil recovery from reservoirs.  However, some LAS present some properties which make them undesired for EOR applications or for the preparation of surfactant concentrates which are later used for preparing the final composition for EOR applications. Some of these undesired properties are high viscosity, high pour point, low solubility of sodium sulfate and / or calcium sulfate, or not achieving a low interfacial tension (IFT) between the crude oil and saline water. Therefore, research is needed to provide LAS compositions which do not present any of those undesired properties. Coming back to the earlier point: the difference between the LAS for household detergent or similar applications and the LAS for EOR application currently on the market is the alkyl length. The LAS currently marketed for household detergent applications usually contain a C10-C13 alkyl chain and is the world’s largest-volume synthetic surfactant with approx. 4.7 million tones being sold on 2022. There are many facilities worldwide with well-established efficient manufacturing process C10-13 LAS. This is well-known from LAB and LAS market analysis. See for example Decode the Future of Linear Alkyl Benzene (LAB) (Sep 2023) in Chemanalyst, https: / / www.chemanalyst.com / industry-report / linear-alkyl-benzene-market-278 and Linear alkyl benzene sulphonic acid (LABSA) in STPP Group, https: / / stppgroup.com / products / detergent-chemicals / labsa / .  On the other hand, the LAS for EOR applications usually contain a C15-C17 alkyl chain. Due to the lower demands of C15-C17 LAS, there are no or only few facilities currently set up for its production. If bigger quantities of C15-C17 LAS are desired, a big investment of energy and building materials is needed to set up new manufacturing plants. Therefore, in view of resource efficiency (i.e. maximizing the benefits of current resources), LAS compositions which can be successfully used in EOR applications, and which are made at least partially from the already-available “detergent” LAS would help minimize the consumption of energy and materials. Further, indirect energy and materials savings may be generated as new manufacturing plants for “EOR” C15-C17 LAS do not need to be set up. And consequently, it would have a positive impact environmentally.  Prior artUS 2009 / 0111717 A1 and WO 2009 / 058889 A1 describe an enhanced oil recovery formulation comprising an alkyl aryl sulfonate as primary surfactant, an aliphatic sulfonate as secondary surfactant, a cosolvent, a passivator, and a polymer.  WO 2009 / 079289 A1 describes an enhanced oil recovery process injecting the surfactant-polymer formulation described in US 2009 / 0111717 A1 and WO 2009 / 058889 A1 through the wellbore into the reservoir and subsequently injecting a chaser solution. WO 2017 / 174770 A1 describes composition and method for an enhanced oil recovery comprising a dialkylated benzene sulfonate salt, an alkyl diphenyl ether disulfonated salt, a polyacrylamide, an alkaline agent and water.  US 2018 / 0057453 A1 describes a process for preparing a surfactant composition comprising dialkyl benzene sulfonates (alkyl moieties independently comprising not more than 15 carbon atoms) and linear alkyl benzene sulfonates.  WO 2014 / 055225 A1 describes a surfactant composition for treating an oil-bearing subterranean formation comprising an alkyl aryl sulfonate salt and a biodegradable chelant comprising ethylenediamine disuccinic acid or its salt.  WO 2013 / 000571 A1 describes a surfactant composition comprising alkyl aryl sulfonate salts and its use in enhanced oil recovery. The alkyl chain of the alkyl aryl sulfonate salt comprises 9 to 10 carbon atoms and at least 20% of the molecules have a branched alkyl chain with a methyl or ethyl group as side chain substituent.  WO 2000 / 037775 A1 describes an enhanced oil recovery process in which an alkyl aryl sulfonate salt, prepared by alkylating aromatic compounds with an alpha-olefin stream having a broad distribution in olefin carbon numbers, is used.  WO 2015 / 138275 A1 describes a surfactant composition, which can comprise alkyl benzene sulfonic acids. Summary of the invention The present invention relates to a composition comprising alkyl benzene sulfonate ABS(I) and ABS(II) (I) (II) wherein R1 and R2 are independently selected from a saturated alkyl group containing from 2 to 13 carbon atoms; R1 and R2 together have a total of 15 carbon atoms;M+ is independently selected from H+, NH4+ or a monovalent cation, preferably a H+, NH4+, Na+ or K+;the molar ratio of ABS(I) : ABS(II) ranges from 10:90 to 30:70.In one embodiment, the composition comprises at least one further alkyl benzene sulfonate molecule selected from ABS(III), ABS(IV), ABS(V) and mixtures thereof, (III) (IV) (V)  whereinM+ is independently selected from a H+, NH4+ or a monovalent cation, preferably a H+, NH4+, Na+ or K+; andthe molar ratio of the alkyl benzene sulfonates [(I)+(II)] : [(III)+(IV)+(V)] ranges from 90:10 to 99.9:0.1;the alkyl benzene sulfonates (I)-(V) together may be referred as ABS mixture “group A”. This invention furthermore relates to concentrated blends and EOR compositions prepared from the inventive ABS composition, their use in oilfield and EOR applications and a method of treating subterranean wellbore with the EOR composition to form a Winsor type III emulsion to successfully recover crude oil.  Surprisingly it was found that the inventive ABS compositions offer several advantages.  Firstly, the inventive ABS compositions (with M+ = H+) are liquid and low viscous at ambient temperature. This facilitates pumping the materials in and out of transportation means (e.g. container trucks) and thus, facilitates the transportation of the ABS compositions to other locations (e.g. remote reservoir). If ABS compositions are not pumpable at high concentrations, they must be diluted for them to be easily pumped in and out of the transportation means. Thus, if a composition has low viscosity even when containing high concentrations of ABS, e.g. higher than 60 wt.%, preferably higher than 80 wt.%, and low water content, e.g. lower than 5 wt.%, preferably lower than 2.5 wt.%, less transportation capacity is needed (e.g. less trucks), in comparison to the situation where a diluted aqueous solution with only ca. 10 – 20 wt% active material is transported. Therefore, high amounts of energy are saved.  Secondly, the inventive ABS compositions (with M+ = H+) have low pour points, i.e. pour points of < -21 ºC. The low viscosity and pour points allow an easy handling of the surfactant composition in remote reservoir locations with limited infrastructure: at ambient conditions no heating is needed to store the mixture and due to the relative low viscosity, and regular pumps can be used. Furthermore, the low pour points also facilitate the handling of the ABS compositions at lower ambient temperatures, such as in winter or in colder regions.  Thirdly, concentrated blends containing high surfactant concentration and low water content having low viscosity at 65 ºC and a pour point lower than 20 ºC can be prepared by mixing the inventive ABS composition (in acidic form), a neutralizing agent and a second surfactant. Beside the delivery of single surfactant components (e.g. ABS composition), also the delivery of surfactant blends as concentrate is an option. For the EOR applications, the alkyl benzene sulfonic acids are neutralized with e.g. Na2CO3 or NaOH to obtain the corresponding sodium salts and they are very often mixed with other surfactants, such as polyalkoxylate-based surfactants. The manufacturing of these concentrated blends may be carried out at a manufacturing location away from the subterranean oil wellbore and therefore, transportation of the concentrated blends is necessary. For the same reasons as explained above, it is desirable that the concentrated blends containing high active surfactant content have low viscosity and low pour points, so that the material can be easily pumped in and out of the transportation means and less transportation capacity and energy is needed. This is achieved by concentrated blends prepared by mixing the inventive ABS composition and at least one further surfactant. Fourthly, clear and stable composition for EOR applications containing between 0.05 to 2 wt.% of surfactants can be prepared from the inventive ABS compositions. EOR compositions comprise at least the alkyl benzene sulfonate salt, any impurities from the ABS preparation step (e.g. sulfonic acid), any remainder of Na2CO3 or NaOH from the neutralization step and, if desired, a second surfactant. For a successful EOR process, it is important that the EOR composition is clear, homogeneous, and stable. If the EOR composition is cloudy and tends to precipitate, for example due to the formation of sodium sulfate (from the remainders of sulfonic acid and Na2CO3 or NaOH) or calcium sulfate (from the remainders of sulfonic acid in contact with formation water comprising bivalent cations, such as calcium cations), there is the risk that the porous reservoir, such as a sandstone or carbonate reservoir, may get plugged and the oil recovery process will be unsuccessful.  The inventive ABS compositions comprise less than 2 wt.% of sulfuric acid. This also contributes to the clear and stable appearance of the ABS compositions and to the reduced risk of plugging the porous reservoir, such as a sandstone or carbonate reservoir.  And fifthly, ultra-low IFT (< 0.01 mN / m) between the crude oil and the saline water can be achieved when EOR compositions prepared from the inventive ABS compositions are used. When EOR compositions, prepared from the inventive ABS compositions, get in contact with crude oil Winsor type III microemulsions are formed. These type of microemulsions enable a very efficient mobilization of crude oil during EOR operations.  In one embodiment of the present invention, the ABS composition further comprises “group B” alkyl benzene sulfonic acids or their salt form, wherein the weight ratio of the ABS mixture “group A” : “group B” ranges from 95:5 to 70:30. These inventive compositions show all the desired properties mentioned above to ABS composition comprising the “group A” ABS.  “Group B” ABS are based on side products / undesired products obtained from the manufacture of C10-C13-Ph, which is the raw material for the synthetic surfactant C10-C13 ABS used e.g. in detergent applications. As already mentioned in the section “Background of the invention”, the C10-C13 ABS are the world’s largest-volume synthetic surfactant currently with approx. 4.7 million tones being sold on 2022. By mixing the “group B” ABS, which is based on an already available alkyl benzene stream, with “group A” ABS, for which currently there are not as many established efficient manufacturing plants, the overall manufacturing needs for “group A” ABS are decreased. Leading to a reduction of the energy and materials required to set up new manufacturing plants for “EOR” C15-C17 LAS. And consequently, having a positive environmental impact. In one embodiment of the present invention, the ABS composition further comprises “group C” alkyl benzene sulfonic acids or their salt form, wherein the weight ratio of the ABS mixture “group A” : “group C” ranges from 25 : 75 to 97.5 : 2.5, preferably from 50 : 50 to 97.5 : 2.5, more preferably from 70 : 30 to 95 : 5, and even more preferable from 85 : 15 to 95: 5. These inventive compositions show all the desired properties mentioned above to ABS composition comprising the “group A” ABS, and additionally it has been surprisingly found that the addition of “group C” ABS surfactants further improves the solubility of the surfactant concentrate in water and reduces viscosities in surfactant concentrates and therefore eases the preparation of the EOR composition.  DefinitionsAs used herein, the following terms have the following meanings unless expressly stated to the contrary: The term “LAB” as used herein refers to a linear alkylbenzene compound.  The term “LAS” as used herein refers to a linear alkylbenzene sulfonic acid or its corresponding salt. The term “ABS” as used herein refers to an alkylbenzene sulfonic acid or its corresponding salt, which may be linear or branched. The terms “enhanced oil recovery” or “EOR” as used herein refer to processes for enhancing the recovery of hydrocarbons from subterranean reservoirs. The terms “active” as used herein refers to the concentration of the surfactant species (i.e., LAS or second surfactant or co-surfactant). The terms “interfacial tension” or “IFT” as used herein refer to the surface tension between test oil and water of different salinities containing a surfactant formulation at different concentrations.  The term “2-alkyl isomer” refers to attachment of the alkyl group on the aromatic ring wherein the longest alkyl chain is attached to the aromatic ring at the 2-position on the alkyl chain. The term “TSP” as used herein refers to tristyrylphenol of technical quality (this means that technical TSP comprises beside tristyrylphenol also minor parts of distyrylphenol and monostyrylphenol). Instead of technical TSP one might speak of styrynated phenol as well. The term “ABS composition” as used herein refers to a composition comprising a high content of alkyl benzene sulfonic acid or its salts as the single surfactant type and low water content. The term “concentrated blend” as used herein refers to a composition comprising a high content of surfactants and low water content, wherein the composition comprises alkyl benzene sulfonated salt and a second surfactant.  The term “EOR composition” as used herein refers to a composition comprising a low content of surfactants, i.e. between 0.05 to 2 wt.%, which is directly injectable into at least one injection well during EOR operations, and wherein the composition comprises at least alkyl benzene sulfonated salt as surfactant and, optionally, a second surfactant. Unless otherwise specified, all percentages are in weight percent and the pressure is in atmospheres. General description of the inventionIn one embodiment of the present invention, the ABS composition comprises alkyl benzene sulfonic acids or their salts according to ABS mixture “group A”. In a further embodiment, the ABS composition additionally comprises alkyl benzene sulfonic acids or their salts according to ABS mixture “group B”, or ABS mixture “group C”, or ABS mixtures “group B” and “group C” . ABS mixture “group A”, “group B” and “group C” will be described below in more detail.  In an embodiment of the present invention, a pumpable concentrated blend can be prepared by mixing any ABS composition comprising alkyl benzene sulfonated salts with a second surfactant or by mixing and ABS composition comprising alkyl benzene sulfonic acid, with a neutralizing agent and a second surfactant.  In an embodiment of the present invention, an EOR composition can be prepared by diluting any ABS composition or concentrated blend with at least water or brine. EOR compositions comprise low surfactant content, i.e. between 0.05 to 2 wt.%, and they can optionally comprise a second surfactant, in addition to the ABS surfactant.  Any composition herein described may comprise additional component selected from a list including, but not limited to, a second surfactant, polymers, solvent, alkaline agents, biocides, oxygen scavengers, anti-scaling agents, and corrosion inhibitors. Suitable examples of these additional components are provided in more detail below.  ABS mixture “Group A”The surfactants of group (A) are selected from the structures ABS (I) – (V).(I) (II)  (III) (IV) (V)  wherein R1 and R2 are independently selected from a saturated alkyl group containing from 2 to 13 carbon atoms; R1 and R2 together have a total of 15 carbon atoms;M+ is independently selected from H+, NH4+ or a monovalent cation, preferably M+ is a H+, NH4+, Na+ or K+. In one embodiment of the present invention, the molar ratio of ABS(I) : ABS(II) in the ABS composition ranges from 10:90 to 30:70, preferably 13:87 to 27:73, more preferably 15:85 to 25:75. In one embodiment of the present invention, the molar ratio of the alkyl benzene sulfonates [(I)+(II)] : [(III)+(IV)+(V)] in the ABS composition ranges from 90:10 to 99.9:0.1. In another embodiment, The ABS composition may comprise other alkyl benzene sulfonate molecules different from ABS mixture “group A”, and in this case, the amount of ABS mixture “group A” is at least 50 wt.%, preferably at least 60 wt.%, more preferably at least 70 wt.%, based on the total weight of all alkyl benzene sulfonate molecules present in the composition. In another embodiment, at least 90% of alkyl chains of the alkyl benzene sulfonic acids or their salts in “group A” are linear, preferably at least 95%. In a preferred embodiment, the SO3M group in ABS(I) and ABS(II) is independently located in ortho or para position, preferably in para position. The surfactants of group (A) can be obtained by alkylation of benzene with a predominately linear C16 alpha olefin using a HF catalyst (alternatively a DETAL catalyst can be used). The alkyl benzene mixture obtained from alkylation of benzene with the alpha olefin having 16 carbon atoms can additionally comprise higher alkylated compounds, which were not removed during the purification step (e.g. distillation). The alkyl benzene mixture obtained is liquid at room temperature and shows a refractive index of 1.479 – 1.482 (at 20 ºC, according to ASTM D-1218). The alkyl benzene mixture can then be sulfonated with sulfonating agent (e.g. sulfur trioxide) in a falling film reactor.  Optionally, the alkyl benzene sulfonic acids can be neutralized with a base (e.g. sodium hydroxide) to form the corresponding salt.  ABS mixture “Group B”The surfactants of group (B) are selected from dialkylated or trialkylated alkylbenzene sulfonic acids or the corresponding salts where sum of all carbon atoms in the alkyl chains predominately ranges from 10 to 20, but none of the alkyl chains has more than 15 carbon atoms, and optionally monoalkylated alkylbenzene sulfonic acids or their salts with a C14-C15 alkyl chain. The surfactants of group (B) are selected from the structure ABS (VI) – (VIII). (VI) (VII) (VIII)  wherein R3 is a saturated alkyl group containing from 14 to 15 carbon atoms; R4, R5, R6, R7, R8 are independently selected from a saturated alkyl group containing at least 2 carbon atoms;the sum of all carbon atoms in R4 and R5 ranges from 10-20 but none of the single alkyl group has more than 15 carbon atoms; the sum of all carbon atoms in R6, R7 and R8 ranges from 10-20 but none of the single alkyl group has more than 15 carbon atoms; M+ is independently selected from a H+, NH4+ or a monovalent cation, preferably a H+, NH4+, Na+ or K+. In one embodiment of the present invention, the weight ratio of the ABS mixture “group A” : “group B” in the ABS composition ranges from 95:5 to 70:30, preferably 90:10 to 70:30, more preferably 85:15 to 75:25. In another embodiment, the molar ratio of the alkyl benzene sulfonates (VI) : [(VII)+(VIII)] in the ABS composition ranges from 0:100 to 20:80. In another preferred embodiment, the content of ABS (VII) is larger than the content of ABS (VIII) in the ABS composition. In a preferred embodiment, at least 50% of alkyl chains of the alkyl benzene sulfonic acids or their salts in “group B” are linear, preferably at least 90%. In one preferred embodiment, the SO3M group is ABS(VI) is in ortho or para position, preferably in para position. For the manufacture of an ABS mixture of “group B”, the alkyl benzene mixture is firstly obtained by the following steps: (1) dehydrogenation of a paraffin mixture with carbon atoms predominately ranging from 10 to 13 to obtain corresponding olefins. Usually, the content of compounds with carbon atoms ranging from 10 to 13 is at least 98%. (2) alkylation of formed olefins with benzene (e.g. using a HF catalyst or a DETAL catalyst). In this step, transalkylation might occur as well,(3) removal of the majority of monoalkylated alkyl benzenes by distillation,(4) distillation of the fraction, which is rich in higher alkylated benzene, and isolation of such a fraction. The boiling point of the first 5% of the desired fraction is min 320 ºC and of the rest 95% is max. 370 ºC (at atmospheric pressure, according to ASTM D-86),(5) the isolated alkyl benzene mixture is liquid at room temperature and shows a refractive index of 1.488 – 1.493 (at 20°C, according to ASTM D-1218)The alkyl benzene mixture can then be sulfonated with sulfonating agent (e.g. sulfur trioxide) in a falling film reactor. Optionally, the alkyl benzene sulfonic acids are neutralized with a base (e.g. sodium hydroxide). An alternative synthetic approach is the mixing of the alkyl benzene compounds, which are the raw material for surfactants from group (A), with the alkyl benzenes, which are the raw material for surfactants from group (B). And then the obtained mixture can be sulfonated with a sulfonating agent (e.g. sulfur trioxide) in a falling film reactor. Optionally, the alkyl benzene sulfonic acids can be neutralized with a base (e.g. sodium hydroxide). ABS mixture “Group C”The surfactants of group (C) are monoalkylated linear alkylbenzene sulfonic acids or the corresponding salts wherein the alkyl chain comprises predominately 10 to 13 carbon atoms. The surfactants of group (C) are selected from the structure ABS (IX). (IX)  wherein R9 is a saturated alkyl group containing 10 to 13 carbon atoms; M+ is a H+, NH4+ or a monovalent cation, preferably a H+, NH4+, Na+ or K+.  In one further embodiment, the ABS(XI)surfactants are selected from ABS(X) and ABS(XI):(X) (XI) wherein R10 is a saturated alkyl group containing 8 to 11 carbon atoms,R11 and R12 are independently selected from a saturated alkyl group containing 2 to 10 carbon atoms, R11 and R12 together have a total of 9 to 12 carbon atoms;M+ is independently selected from H+, NH4+ or a monovalent cation; preferably a H+, NH4+, Na+ or K+. In one embodiment of the present invention, the ABS composition comprises ABS mixtures “group A” and “group C” and the weight ratio of the ABS mixture “group A” : “group C” ranges from 25 : 75 to 97.5 : 2.5, preferably from 50 : 50 to 97.5 : 2.5, more preferably from 70 : 30 to 95 : 5, and even more preferable from 85 : 15 to 95: 5. In another embodiment of the present invention, the ABS composition comprises ABS mixtures “group A”, “group B” and “group C” and the weight ratio of ABS mixture (“group A”+ “group B”) : “group C” ranges from 80:20 to 97.5:2.5, preferably 85:15 to 97.5:2.5, more preferably 85:15 to 95:5. In another embodiment of the present invention, the weight ratio of ABS(X) : ABS(XI) in the ABS composition ranges from 10:90 to 25:75, preferably 14:86 to 21:79. In a preferred embodiment, at least 90% of alkyl chains of the alkyl benzene sulfonic acids or their salts in “group C” are linear, preferably at least 95%. In one preferred embodiment, the SO3M group is ABS(IX)-ABS(XI) is independently located in ortho or para position, preferably in para position. ABS surfactants of “group C” can obtained by (a) dehydrogenation of a paraffin mixture with carbon atoms predominately ranging from 10 to 13 to obtain olefins, the content of compounds with carbon atoms ranging from 10 to 13 is at least 98%, or (b) obtaining a suitable mixture of linear olefins containing predominately C10-C13 carbon atoms, from ethylene oligomerization and olefin metathesis. The obtained olefines are alkylated with benzene (using a HF catalyst or a DETAL catalyst), followed by distillation. The boiling point of the first 5% of the monoalkylated benzene mixture obtained from the distillation process is min 280 ºC and for the rest 95% is max. 310 ºC (at atmospheric pressure, according to ASTM D-86). The distilled monoalkylated benzene fraction is liquid at room temperature and shows a refractive index of 1.481 – 1.485 (at 20 ºC, according to ASTM D-1218). The distilled monoalkylated benzene mixtures have an average molecular weight ranging from 238 to 243 g / mol.  Then the monoalkylated benzene fraction is sulfonated with a sulfonating agent (e.g. sulfur trioxide) in a falling film reactor. Optionally, the alkyl benzene sulfonic acids are neutralized with a base (e.g. sodium hydroxide). Further additives The initial ABS composition, the concentrated blend or the EOR composition may further comprise one or more additives selected from:a second or further surfactants, different from any of the surfactants ABS (I) – (XI), polymers,solvent,alkaline agents, biocides, oxygen scavengers,radical scavengers, anti-scaling agents, andcorrosion inhibitors. The compositions may optionally comprise a second or further surfactants, different from any of the surfactants ABS (I) – (XI) as already described. These second or further surfactants can include one or more anionic, nonionic, cationic, or amphoteric surfactants generally known in the art to be effective in reducing the interfacial tension between a composition injected into an oil-bearing subterranean formation for recovering oil and the residual oil. Cationic surfactants may also be employed; however, they are usually less effective and more costly. Examples of anionic surfactants include, but are not limited to aryl ether sulfates, alkyl ether sulfates, alkyl ether sulfonates, alkyl ether hydroxpropylsulfonates, aryl ether carboxylates, alkyl ether carboxylates, carboxymethylated alkyl poly glucosides, alkylphenol ether sulfonates, alkyl diphenylether disulfonates, sulfonated alpha-olefins, and sulfonated internal olefins. Examples of nonionic surfactants include, but are not limited to alkoxylated alkylphenols, alkoxylated linear or branched alcohols, and alkyl polyglucosides. Cationic surfactants include, but are not limited to, alkyl trimethylammonium chlorides or alkyl trimethylammonium bromides. Amphoteric surfactants include, but are not limited to betaines, sulfobetaines, amidopropyl betaines, and amine oxides.  In one embodiment, the composition of the present invention is free of [Glu1, Asp5]-C15 surfactin. In a further embodiment, the composition of the present invention is free from biosurfactant. The compositions may optionally comprise a polymer. Examples of polymers include, but are not limited to, high molecular weight acrylic acid- acrylamide copolymers, acrylic acid-acrylamide-diacetone acrylamide terpolymers, acrylic acid-acrylamide-AMPS-terpolymers, partially hydrolyzed polyacrylamides, hydroxyethyl cellulose, carboxymethyl cellulose, polyacrylamides, polyoxyethylenes, modified starches, heteropolysaccharides obtained by fermentation of starch derived sugar, polyvinyl alcohol, polyvinyl pyrrolidone and polystyrene sulfonates. The compositions may optionally comprise a solvent. Examples of suitable solvents include, but are not limited to alcohols, such as lower carbon chain alcohols, for example, isopropyl alcohol, ethanol, n-propyl alcohol, n-butyl alcohol, sec-butyl alcohol, n-amyl alcohol, sec-amyl alcohol, n-hexyl alcohol, and sec-hexyl alcohol; alcohol ethers, polyalkylene alcohol ethers, such as ethylene glycol monobutyl ether or diethylene glycol monobutyl ether, polyalkylene glycols, such as ethylene glycol and propylene glycol, poly(oxyalkylene) glycols, such as diethylene glycol, poly(oxyalkylene) glycol ethers, or any mixtures thereof. The compositions may optionally comprise an alkaline agent. Example of suitable alkaline agents include, but are not limited to, sodium metaborate, sodium hydroxide, sodium tetraborate or sodium carbonate.  The compositions may optionally comprise a biocide. Example of suitable biocides include, but are not limited to, glutaraldehyde and quaternary ammonium compounds, especially those containing long alkyl chains which can be derived from fatty acids, having antimicrobial activity. Examples of such quaternary ammonium compounds are compounds containing at least one of benzalkonium, benzethonium, methylbenzethonium, cetalkonium, cetylpyridinium, cetrimonium, cetrimide, dofanium, tetraethylammonium, didecyldimethylammonium and domiphen as the quaternary ammonium ions and chloride or bromide as the anion. The compositions may optionally comprise an oxygen scavenger. Oxygen scavengers react with oxygen which may possibly be present in the aqueous formulation and thus prevent the oxygen from being able to attack the polymer or polyether groups. Examples of oxygen scavengers comprise sulfites, for example Na2S03, bisulfites, phosphites, hypophosphites or dithionites.  The compositions may optionally comprise an anti-scaling agent. Example of suitable anti-scaling agents include, but are not limited to, phosphonate compounds (hexamethylene tetramethylene phosphonate (HMDP), diethylenetriamine penta (methylphosphonate) (DETPMP) , bis (hexamethylene) triamine pentabis (methylene phosphonate) (HMTPMP), nitrilotris ( (methylene) tri phosphonate (NTP) , pentaethylene hexamineoctakis- (methylene phosphonate) (PEHOMP) , for instance) and / or poly-phosphino carboxylic acid (PPCA) . Application of the EOR composition In one embodiment of the present invention, an EOR composition comprising water, the surfactants ABS “group A”, optionally the surfactants “group B” and / or “group C”, a basic ionic salt and a second surfactant, which is different from any of surfactants ABS (I)-(IX) is prepared. The total active surfactant present in the EOR composition is between 0.05 to 2 wt.%, in respect of the total weight of the EOR composition. The EOR composition can be used in an oilfield or enhanced oil recovery (EOR) application. In a preferred embodiment, the EOR composition is use as EOR surfactant, flow back improver, wetting agent, dispersant, emulsifying agent, drilling fluid, fracturing fluid, spacer fluid, drill cutting cleaner, well bore cleaner and foamer for drilling fluids. A further embodiment of this invention is a process for recovering oil from an oil-bearing subterranean formation comprising injecting the above-mentioned EOR composition into one or more injection wells, forming a Winsor type III microemulsion, achieving an interfacial tension between crude oil and aqueous surfactant solution of <0.1 mN / m and producing oil from one or more producing wells. The oil-bearing subterranean formation may contain sandstone or carbonate reservoirs with reservoir temperatures from 15 to 130 ºC. In a preferred embodiment of the invention, the deposit is a sandstone deposit, wherein more than 70 percent by weight of sand (quartz and / or feldspar) is present and up to 25 percent by weight of other minerals selected from kaolinite, smectite, illite, chlorite and / or pyrite may be present. It is preferable that more than 75 percent by weight of sand (quartz and / or feldspar) is present and up to 20 percent by weight of other minerals selected from kaolinite, smectite, illite, chlorite and / or pyrite may be present. It is especially preferable that more than 80 percent by weight of sand (quartz and / or feldspar) is present and up to 15 percent by weight of other minerals selected from kaolinite, smectite, illite, chlorite and / or pyrite may be present. The API gravity (American Petroleum Institute gravity) is a conventional unit of density commonly used in the USA for crude oils. It is used globally for characterization and as a quality standard for crude oil. The API gravity is calculated from the relative density prel of the crude oil at 60°F (15.56°C), based on water, usingAPI gravity = (141.5 / prel) – 131.5. According to the invention, the crude oil from the deposit should have at least 10° API. Preference is given to at least 12° API. Particular preference is given to at least 15° API. Very particular preference is given to at least 20° API. To execute the method of the invention, at least one production well and at least one injection well are sunk into the mineral oil deposit. In general, a deposit is provided with several injection wells and with several production wells. An aqueous formulation of the water-soluble components described is injected through the at least one injection well into the mineral oil deposit, and crude oil is withdrawn from the deposit through at least one production well. As a result of the pressure generated by the aqueous formulation injected, called the "flood", the mineral oil flows in the direction of the production well and is produced via the production well.  The term „crude oil” or “mineral oil” in this context of course does not just mean single-phase oil; instead, the term also encompasses the usual crude oil-water emulsions. It will be clear to the person skilled in the art that a mineral oil deposit may also have a certain temperature distribution. Said deposit temperature is based on the region of the deposit between the injection and production wells which is covered by the flooding with aqueous solutions. Methods of determining the temperature distribution of a mineral oil deposit are known in principle to those skilled in the art. The temperature distribution is generally determined from temperature measurements at particular sites in the formation in combination with simulation calculations; the simulation calculations also take account of the amounts of heat introduced into the formation and the amounts of heat removed from the formation. The injecting of the EOR composition can be undertaken by means of customary apparatuses. The composition can be injected into one or more injection wells by means of customary pumps. The injection wells are typically lined with steel tubes cemented in place, and the steel tubes are perforated at the desired point. The formulation enters the mineral oil formation from the injection well through the perforation. The pressure applied by means of the pumps, in a manner known in principle, is used to fix the flow rate of the formulation and hence also the shear stress with which the aqueous formulation enters the formation. The shear stress on entry into the formation can be calculated by the person skilled in the art in a manner known in principle based on the Hagen-Poiseuille law, using the area through which the flow passes on entry into the formation, the mean pore radius and the volume flow rate. The average permeability of the formation can be found as described in a manner known in principle. Naturally, the greater the volume flow rate of EOR composition injected into the formation, the greater the shear stress. The rate of injection can be fixed by the person skilled in the art according to the conditions in the formation.  The above-described method of crude oil production with the aid of the EOR composition comprising water, the surfactants ABS “group A”, and optionally the surfactants “group B” and / or “group C”, can optionally be conducted with the addition of further methods. For instance, it is optionally possible to add a polymer or a foam for mobility control. The polymer can optionally be injected into the deposit together with the surfactant formulation, followed by the surfactant formulation. It can also be injected only with the surfactant formulation or only after surfactant formulation. The polymers may be copolymers based on acrylamide or a biopolymer. The copolymer may consist, for example, of the following units inter alia:  - acrylamide and acrylic acid sodium salt - acrylamide and acrylic acid sodium salt and N-vinylpyrrolidone- acrylamide and acrylic acid sodium salt and AMPS (2-acrylamido-2-methylpropanesulfonic acid sodium salt)- acrylamide and acrylic acid sodium salt and AMPS (2-acrylamido-2-methylpropanesulfonic acid sodium salt) and N-vinylpyrrolidone. The copolymer may also additionally comprise associative groups. Usable copolymers are described in EP 2432807 or in WO 2014095621. Further usable copolymers are described in US 7700702.  ExamplesIn the following inventive and comparative examples, several alkyl benzene sulfonic acid compositions, concentrated blends and EOR compositions have been prepared and tested. The preparation of these composition and the testing methods are described below. The experimental results obtained from the tests are collected in Table 1. The following examples are presented to illustrate specific embodiments of this invention and are not to be constructed in any way as limiting the scope of the invention. The alkylation of benzene is described by S. Karimi et al in Russian Journal of Applied Chemistry2021, Vol. 94, No. 11, pp. 1546–1559. Preparation of ABS composition for comparative example 1 (C1):In a first step, a C16 alpha olefin (95% linearity, 99% C16 content, 95% alpha olefin content) is reacted with benzene using AlCl3 as catalyst. Unreacted raw materials are removed by distillation. Analysis of the obtained alkyl benzene mixture (via proton NMR spectroscopy, carbon NMR spectroscopy, gas chromatography, and mass spectroscopy) shows a 2-phenyl-isomer content of 36% and a monoalkylation degree of 99.7%. The content of benzene was <100 ppm.  In a second step, 1.0 eq of the obtained C16-Ph are converted with ca. 1.03 eq of sulfur trioxide in a falling film reactor (glass reactor, 1 m length) at 50°C in presence of a nitrogen flow. The C16-Ph flows from top to the bottom of the glass reactor. Thereby, a film of organic material is formed. The nitrogen stream is adjusted in such a way that small waves are generated on the organic film. The nitrogen stream comprises ca. 1.03 eq of gaseous sulfur trioxide. At the bottom of the reactor the obtained liquid is collected and stored for 2 hours at 50°C. The sulfonation reaction is quenched by addition of 0.3 – 0.5 wt% water. The obtained material is analyzed by proton NMR spectroscopy (for ABS and alkyl benzene content determination), carbon NMR spectroscopy (for ABS and alkyl benzene content determination), gas chromatography and HPLC (both for ratio of structures determination), ion chromatography (for sulfuric acid content determination), titration with hyamine (for anionic surfactant content determination) and by Karl Fischer analysis (for water content determination). Obtained composition, C1:95.7 wt.% total ABS contentmol. Ratio (I):(II) 36:64mol. ratio [(I)+(II)]:[(III)+(IV)+(V)] 99.7:0.3ABS content (I)-(V), whereinM+ = H+1.6 wt.% alkyl benzene 1.9 wt.% sulfuric acid 0.8 wt.% water  Preparation of ABS composition for inventive example 2: In a first step, a C16 alpha olefin (95% linearity, 99% C16 content, 95% alpha olefin content) is reacted with benzene using HF as catalyst. Unreacted raw materials are removed by distillation and the desired alkyl benzene mixture is kept. Analysis of the obtained alkyl benzene mixture (via proton NMR spectroscopy, carbon NMR spectroscopy, gas chromatography, and mass spectroscopy) shows a 2-phenyl-isomer content of 17% and a monoalkylation degree of 98.7%. The content of benzene was <100 ppm.  In a second step, 1.0 eq of the obtained C16-Ph are converted with ca. 1.03 eq of sulfur trioxide in a falling film reactor (glass reactor, 1 m length) at 50°C in presence of a nitrogen flow. The C16-Ph flows from top to the bottom of the glass reactor. Thereby, a film of organic material is formed. The nitrogen stream is adjusted in such a way that small waves are generated on the organic film. The nitrogen stream comprises ca. 1.03 eq of gaseous sulfur trioxide. At the bottom of the reactor the obtained liquid is collected and stored for 2 hours at 50°C. The sulfonation reaction is quenched by addition of 0.3 – 0.5 wt% water. The obtained material is analyzed by proton NMR spectroscopy (for ABS and alkyl benzene content determination), carbon NMR spectroscopy (for ABS and alkyl benzene content determination), gas chromatography and HPLC (both for ratio of structures determination), ion chromatography (for sulfuric acid content determination), titration with hyamine (for anionic surfactant content determination) and by Karl Fischer analysis (for water content determination). Obtained composition, example 2:93.9 wt.% total ABS contentmol. Ratio (I):(II) 17:83mol. ratio [(I)+(II)]:[(III)+(IV)+(V)] 98.7:1.3ABS content (I)-(V), whereinM+ = H+3.9 wt.% alkyl benzene 1.4 wt.% sulfuric acid 0.8 wt.% water  Preparation of ABS composition for comparative example 3 (C3):In a first step, the so-called Heavy-Alkyl-Benzene (HAB) fraction from detergent production was used.  The Heavy-Alkyl-Benzene fraction is obtained in the following way: a paraffin fraction, which predominately comprises 10 to 13 carbon atoms, was partially dehydrogenated and the obtained olefin (mainly mono-olefin and mainly linear) was reacted with benzene using HF as catalyst. The alkyl benzene mixture was purified from unreacted raw materials. Then the fraction of C10-C13 monoalkylated alkyl benzene was removed by distillation. This fraction of monoalkylated alkyl benzene predominately comprises 10 to 13 carbon atoms in the alkyl chain, has an average molecular weight from 242 g / mol, a 2-phenyl isomer content of 15% a boiling range at 1 atm absolute of 288°C (for the first 5% of the fraction) to 304°C (for 95% of the fraction).  After removal of the fraction of C10-C13 monoalkylated benzene, the so-called Heavy-Alkyl-Benzene fraction (HAB fraction) is left over. From this HAB fraction, the components with lower boiling points were isolated by distillation. The desired fraction was characterized in such a way that at 1 atm absolute pressure boiling point ranges from 329°C (for first 5%) to 350°C (for 95%). the obtained alkyl benzene mixture is analyzed (via proton NMR spectroscopy, carbon NMR spectroscopy, gas chromatography and mass spectroscopy). The content of monoalkylated alkyl benzene, comprising 14 to 15 carbon atoms in the alkyl group, was around 10%. The sum of the carbon atoms in the alkyl groups in the twofold and threefold alkylated benzenes ranges from 12 to 18 while none of a single alkyl group of the multi-alkylated benzene comprises more than 15 carbon atoms.  The obtained fraction was sulfonated in a second step. 1.0 eq of the obtained alkyl benzene are converted with ca. 1.03 eq of sulfur trioxide in a falling film reactor (glass reactor, 1 m length) at 50°C in presence of a nitrogen flow. The alkyl benzene flows from top to the bottom of the glass reactor. Thereby, a film of organic material is formed. The nitrogen stream is adjusted in such a way that small waves are generated on the organic film. The nitrogen stream comprises ca. 1.03 eq of gaseous sulfur trioxide. At the bottom of the reactor the obtained liquid is collected and stored for 2 hours at 50°C. The sulfonation reaction is quenched by addition of 0.3 – 0.5 wt% water. The obtained material is analyzed by proton NMR spectroscopy (for ABS and alkyl benzene content determination), carbon NMR spectroscopy (for ABS and alkyl benzene content determination), gas chromatography and HPLC (both for ratio of structures determination), ion chromatography (for sulfuric acid content determination), titration with hyamine (for anionic surfactant content determination) and by Karl Fischer analysis (for water content determination). Obtained composition, C3:90 wt.% total ABS contentmol. Ratio (VI):[(VII)+(VIII)] 10:901 ABS content: (VI)-(VIII), whereinM+ = H+,R3 = C14-C15R4+R5 = C12-C18R6+R7+R8 = C12-C187 wt.% alkyl benzene 2.7 wt.% sulfuric acid 0.3 wt.% water 1 margin of error ±52 according to ASTM D-86 Preparation of ABS composition for comparative example 4 (C4):In a 250 ml round bottom glass flask with stirrer, 100 g of an ABS mixture was prepared at 50°C by mixing the ABS composition from C1 (45 g) and the ABS composition from C3 (55 g). Both ABS compositions were added into the flask, stirred at 50°C for 1 hour and a homogeneous mixture was obtained. Obtained composition, C4:92.6 wt.% total ABS content,mol. ratio (I):(II) 36:64mol. ratio [(I)+(II)]:[(III)+(IV)+(V)] 99.7:0.3mol. ratio (VI):[(VII)+(VIII)] 10:901wt. ratio “group A”:”group B” 46.5:53.5 ABS content: (I)-(VIII), wherein M+ = H+R3 = C14-C15R4+R5 = C12-C18R6+R7+R8 = C12-C184.6 wt.% alkyl benzene 2.3 wt.% sulfuric acid 0.5 wt.% water 1margin of error ±5 Preparation of ABS composition for inventive example 5:In a first step a mixture of alkyl benzenes was prepared. A C16 alpha olefin (95% linearity, 99% C16 content, 95% alpha olefin content) is reacted with benzene using HF as catalyst. Unreacted raw materials are removed by distillation. Analysis of the obtained alkyl benzene mixture (via proton NMR spectroscopy, carbon NMR spectroscopy, gas chromatography, and mass spectroscopy) shows a 2-phenyl-isomer content of 17% and a monoalkylation degree of 97.7%. The content of benzene was <100 ppm. 800 g of this C16 alkyl benzene was mixed at 50 °C in a glass vessel with stirrer with 200 g of the alkyl benzene mixture obtained during the first step of example C3 (that means the alkyl benzene mixture obtained before the sulfonation step in C3). In a second step, the 80:20 mixture of the alkyl benzenes (80 wt% of the C16-alkyl benzene and 20 wt% of the C12-C18 alkyl benzene) was sulfonated. 1.0 eq of the 80 : 20 alkyl benzene mixture is reacted with ca. 1.03 eq of sulfur trioxide in a falling film reactor (glass reactor, 1 m length) at 50°C in presence of a nitrogen flow. The alkyl benzene flows from top to the bottom of the glass reactor. Thereby, a film of organic material is formed. The nitrogen stream is adjusted in such a way that small waves are generated on the organic film. The nitrogen stream comprises ca. 1.03 eq of gaseous sulfur trioxide. At the bottom of the reactor the obtained liquid is collected and stored for 2 hours at 50°C. The sulfonation reaction is quenched by addition of 0.3 – 0.5 wt% water. The obtained material is analyzed by proton NMR spectroscopy (for ABS and alkyl benzene content determination), carbon NMR spectroscopy (for ABS and alkyl benzene content determination), gas chromatography and HPLC (both for ratio of structures determination), ion chromatography (for sulfuric acid content determination), titration with hyamine (for anionic surfactant content determination) and by Karl Fischer analysis (for water content determination). Obtained composition, example 5:92.8 wt.% total ABS content,mol. ratio (I):(II) 17:83mol. ratio [(I)+(II)]:[(III)+(IV)+(V)] 97.7:2.3mol. ratio (VI):[(VII)+(VIII)] 10:901wt. ratio “group A”:”group B” 80:20ABS content: (I)-(VIII), wherein M+ = H+R3 = C14-C15R4+R5 = C12-C18R6+R7+R8 = C12-C185.4 wt.% alkyl benzene 0.9 wt.% sulfuric acid 0.9 wt.% water 1margin of error ±5 Preparation of ABS composition for inventive example 6:The ABS composition comprising detergent surfactant C10-C13-Ph-SO3H was obtained in the following way: In a first step, a paraffin fraction, which predominately comprises 10 to 13 carbon atoms, was partially dehydrogenated and the obtained olefin (mainly mono-olefin and mainly linear) was reacted with benzene using HF as catalyst. Unreacted raw materials are removed by distillation. Then the fraction of C10-C13 monoalkylated alkyl benzene was removed by distillation. This fraction of monoalkylated alkyl benzene predominately comprises 10 to 13 carbon atoms in the alkyl chain (11.6 carbon atoms on average), has an average molecular weight from 241 g / mol, a 2-phenyl isomer content of 15% a boiling range at 1 atm absolute of 288°C (for the first 5% of the fraction) to 304°C (for 95% of the fraction).  In a second step, the obtained C10-C13 ABS mixture was sulfonated. 1.0 eq of the obtained alkyl benzene are converted with ca. 1.03 eq of sulfur trioxide in a falling film reactor (glass reactor, 1 m length) at 50°C in presence of a nitrogen flow. The alkyl benzene flows from top to the bottom of the glass reactor. Thereby, a film of organic material is formed. The nitrogen stream is adjusted in such a way that small waves are generated on the organic film. The nitrogen stream comprises ca. 1.03 eq of gaseous sulfur trioxide. At the bottom of the reactor the obtained liquid is collected and stored for 2 hours at 50°C. The sulfonation reaction is quenched by addition of 0.3 – 0.5 wt.% water. The obtained material is analyzed by proton NMR spectroscopy (for ABS and alkyl benzene content determination), carbon NMR spectroscopy (for ABS and alkyl benzene content determination), gas chromatography and HPLC (both for ratio of structures determination), ion chromatography (for sulfuric acid content determination), titration with hyamine (for anionic surfactant content determination) and by Karl Fischer analysis (for water content determination). Finally, in a 250 ml round bottom glass flask with stirrer, 100 g of an ABS mixture was prepared at 50°C by mixing the ABS composition from example 5 (92.5 g) with the prepared ABS composition comprising detergent surfactant C10-C13-Ph-SO3H (7.5 g). Both ABS were added into the flask, stirred at 50°C for 1 hour and a homogeneous mixture was obtained. The obtained material is analyzed by proton NMR spectroscopy (for ABS and alkyl benzene content determination), carbon NMR spectroscopy (for ABS and alkyl benzene content determination), gas chromatography and HPLC (both for ratio of structures determination), ion chromatography (for sulfuric acid content determination), titration with hyamine (for anionic surfactant content determination) and by Karl Fischer analysis (for water content determination).Obtained composition, example 6:93.1 wt.% total ABS content,mol. ratio (I):(II) 17:83mol. ratio [(I)+(II)]:[(III)+(IV)+(V)] 97.7:2.3mol. ratio (VI):[(VII)+(VIII)] 10:901wt. Ratio (X):(XI) 15:85wt. ratio “group A”:”group B” 80:20wt. ratio groups A:B:C 74:18.5:7.5ABS content: (I)-(VIII) and (X)-(XI), wherein M+ = H+R3 = C14-C15R4+R5 = C12-C18R6+R7+R8 = C12-C18R10 = C8-C11 (average ca. 9.6)R11+R12 = C9-C12 (average ca. 10.6)5.2 wt.% alkyl benzene 0.9 wt.% sulfuric acid 0.8 wt.% water 1margin of error ±5 Preparation of ABS composition for inventive example 7:The ABS composition comprising detergent surfactant C10-C13-Ph-SO3H was obtained in the following way: In a first step, a paraffin fraction, which predominately comprises 10 to 13 carbon atoms, was partially dehydrogenated and the obtained olefin (mainly mono-olefin and mainly linear) was reacted with benzene using HF as catalyst. Unreacted raw materials are removed by distillation. Then the fraction of C10-C13 monoalkylated alkyl benzene was removed by distillation. This fraction of monoalkylated alkyl benzene predominately comprises 10 to 13 carbon atoms in the alkyl chain (11.6 carbon atoms on average), has an average molecular weight from 241 g / mol, a 2-phenyl isomer content of 15% a boiling range at 1 atm absolute of 288°C (for the first 5% of the fraction) to 304°C (for 95% of the fraction).  In a second step, the obtained C10-C13 ABS mixture was sulfonated. 1.0 eq of the obtained alkyl benzene are converted with ca. 1.03 eq of sulfur trioxide in a falling film reactor (glass reactor, 1 m length) at 50°C in presence of a nitrogen flow. The alkyl benzene flows from top to the bottom of the glass reactor. Thereby, a film of organic material is formed. The nitrogen stream is adjusted in such a way that small waves are generated on the organic film. The nitrogen stream comprises ca. 1.03 eq of gaseous sulfur trioxide. At the bottom of the reactor the obtained liquid is collected and stored for 2 hours at 50°C. The sulfonation reaction is quenched by addition of 0.3 – 0.5 wt.% water. The obtained material is analyzed by proton NMR spectroscopy (for ABS and alkyl benzene content determination), carbon NMR spectroscopy (for ABS and alkyl benzene content determination), gas chromatography and HPLC (both for ratio of structures determination), ion chromatography (for sulfuric acid content determination), titration with hyamine (for anionic surfactant content determination) and by Karl Fischer analysis (for water content determination). Finally, in a 250 ml round bottom glass flask with stirrer, 100 g of an ABS mixture was prepared at 50°C by mixing the ABS composition from example 2 (92.5 g) with the prepared ABS composition comprising detergent surfactant C10-C13-Ph-SO3H (7.5 g). Both ABS were added into the flask, stirred at 50°C for 1 hour and a homogeneous mixture was obtained. The obtained material is analyzed by proton NMR spectroscopy (for ABS and alkyl benzene content determination), carbon NMR spectroscopy (for ABS and alkyl benzene content determination), gas chromatography and HPLC (both for ratio of structures determination), ion chromatography (for sulfuric acid content determination), titration with hyamine (for anionic surfactant content determination) and by Karl Fischer analysis (for water content determination).Obtained composition, example 7:94.1 wt.% total ABS content,mol. ratio (I):(II) 17:83mol. ratio [(I)+(II)]:[(III)+(IV)+(V)] 98.7:1.3wt. Ratio (X):(XI) 15:85wt. ratio groups A:B:C 92.5:0:7.5ABS content: (I)-(VIII) and (X)-(XI), wherein M+ = H+R3 = C14-C15R4+R5 = C12-C18R6+R7+R8 = C12-C18R10 = C8-C11 (average ca. 9.6)R11+R12 = C9-C12 (average ca. 10.6)5.2 wt.% alkyl benzene 0.9 wt.% sulfuric acid 0.8 wt.% water 1margin of error ±5   Preparation of the concentrated blendsTo prepare concentrated blends containing high active surfactant content and low water content, the alkyl benzene sulfonic acids prepared in the comparative examples 1, 3 and 4 and inventive examples 2, 5, 6 and 7 are neutralized with 50 wt.% NaOH in water in the presence of TSP-(PO)35-(EO)20-SO4NH4 (polyalkoxylate-based surfactant). The obtained concentrated blends have a pH of at least 7.5.  Preparation of TSP-(PO)35-(EO)20-SO4NH4:Styrynated phenol (80% tristyrylphenol, 15% distyrylphenol and 5% monostyrylphenol) is firstly propoxylated with 35 eq. of propylene oxide and secondly ethoxylated with 20 eq. of ethylene oxide using KOH catalysis at 130 ºC. Then it is sulfated with sulfamic acid in the presence of catalytic amounts of urea at 95 ºC. A sulfation degree of 98% is obtained according to 1H-NMR. The obtained TSP-(PO)35-(EO)20-SO4NH4 has an active content of 98%, a pour point of < 20 ºC and a viscosity of 9000 – 14000 mPas at 25 ºC. The exact weight ratio of the active ABS surfactant (in acidic form), the TSP-(PO)35-(EO)20-SO4NH4 and the aq. sol. of 50 wt.% NaOH used for each concentrated blend is indicated in Table 1. In all cases the weight ratio between the TSP-(PO)35-(EO)20-SO4NH4 to the active ABS (in acidic form) in the concentrated blend is approximately 1.5 : 1. This equals to a weight ratio of 1.5 : 1.056 between the TSP-(PO)35-(EO)20-SO4NH4 to the active ABS (in salt form, i.e. due to the neutralization of the ABS with sodium hydroxide). Preparation of the EOR composition To prepare the EOR composition, the concentrated blend is dissolved in brine until obtaining the desired surfactant concentration: 2556 ppm of active surfactant (1500 ppm of TSP-(PO)35-(EO)20-SO4NH4 + 1056 ppm of active ABS (in salt form). The brine used for the appearance / solubility tests is made of water, 0.45% NaCl, 0.01% KCl, 0.1% NaHCO3, 0.05% Na2SO4 and 2.75% Na2CO3. The brine used for the IFT tests is made of water, 0.45% NaCl, 0.01% KCl, 0.1% NaHCO3, 0.05% Na2SO4 and 2.5% Na2CO3. Viscosity measurementsThe viscosity of the alkyl benzene sulfonic acid compositions and the concentrated blends was measured. An Anton Parr viscosimeter with double gap geometry was used. The results are shown in Table 1. A viscosity of < 5000 mPas at 25 ºC and 10 s-1 indicates that the material is pumpable.   Pour point measurementsThe pour point of the alkyl benzene sulfonic acid compositions and the concentrated blends was measured according to ASTM D7346. The results are shown in Table 1. Low pour points indicates that the material can still flow and be pumpable at lower temperatures. Evaluation of the appearance of EOR composition at 65 ºCThe solubility of the alkyl benzene sulfonate salts combined with TSP-(PO)35-(EO)20-SO4NH4 in presence of Na2CO3 at 65 ºC was investigated.  To use the alkyl benzene sulfonic acids in EOR applications, they are neutralized with e.g. Na2CO3 or NaOH in order to obtain the corresponding salts.  The EOR composition will comprise at least the alkyl benzene sulfonate salt, any impurities from the ABS preparation step (e.g. sulfonic acid), any remainder of Na2CO3 or NaOH from the neutralization step and, if desired, a second surfactant. For a successful EOR process, it is important that the EOR composition is clear, homogeneous and stable. If the EOR composition is cloudy and tends to precipitate, for example due to the formation of sodium sulfate (from the remainders of sulfonic acid and Na2CO3 or NaOH) or calcium sulfate (from the remainders of sulfonic acid in contact with formation water comprising bivalent cations, such as calcium cations), there is the risk that the porous reservoir may get plugged and the oil recovery process will be unsuccessful.  The evaluation was carried out visually. Interfacial tension (IFT) measurements of EOR composition and crude oilThe interaction between 10 vol.% of crude oil (from Northwest of India, rich in paraffin) and 90 vol% of the EOR compositions was investigated. An EOR composition comprising only 2.5% of Na2CO3 was used so that solubility and optimum phase behaviour match. After storage of days or weeks at optimum conditions without stirring the Winsor type III microemulsion is formed. In a Winsor type III microemulsion, ultralow interfacial tensions of typically <0.01 mN / m are achieved. From phase behaviour tests one obtains the SP* and can calculate the interfacial tension using the Huh equation. Measurements were done at 65 ºC.Examplemol. ratio ABS (I):(II) ;wt. ratio ABS mixture A : B : CViscosity of ABS composition at 25ºC [mPas]Pour point ABS composition [ºC]Concentrated blend1,wt. ratio of second surfactant : ABS surfactant : aq. sol. of 50 wt.% NaOHViscosity of the concentrated blend1[mPas] Pour point of the concentrated blend1 [ºC]Appearance at 65 ºC of EOR composition2, comprising the ABS surfactant and a second surfactant2 IFT at 65 ºC of 10 vol.% crude oil4 and 10 vol.% EOR composition3[mN / m]C136 : 64100 : 0 : 0820-9 52.7 : 36.7 : 10.66> 5000> 40Clear> 0.1217:83100 : 0: 0920-3053.3 : 37.9 : 8.8< 1000 < 20 Clear< 0.01C3N / A0 : 100 : 02200-21n.d.n.d.n.d.Cloudyn.d.5C436 : 6446.5:53.5:01600-1551.8 : 37.3 : 10.96> 5000> 40Clear< 0.01517:8380 : 20 : 0970-3353.3 : 38.2 : 8.5700< 20Clear< 0.01617:8374 : 18.5: 7.5980-3353.3 : 38.2 : 8.5 650< 20Clear< 0.01717:8392.5 : 0: 7.5910-3053.3 : 37.9 : 8.8< 1000< 20Clear< 0.01Table 1: Experimental results from the ABS compositions, the concentrated blends and the EOR composition1Concentrated blend prepared by mixing the ABS composition, TSP-(PO)35-(EO)20-SO4NH4 used as second surfactant and an aqueous solution of 50 wt.% of NaOH in the indicated amounts.2 EOR composition: 1500 ppm of TSP-(PO)35-(EO)20-SO4NH4, 1056 ppm of active neutralized ABS surfactant and brine comprising water, 0.45% NaCl, 0.01% KCl, 0.1% NaHCO3, 0.05% Na2SO4 and 2.75% Na2CO3. 3EOR composition: same as above, but brine comprises 2.5% of Na2CO3.4Crude oil from Northwest of India, rich in paraffin 5n.d. = not determined 6unwanted foam formation was observed (due to release of some ammonia) and additional NaOH solution was needed to fully neutralize the ABS composition.Comments about the experimental results shown in Table 1: There are mainly two ways to obtain an EOR composition comprising between 0.05 to 2 wt.% of surfactants, including at least an ABS surfactant, ready to use at the reservoir location. Note that for EOR operations, the alkyl benzene sulfonic acids shall be neutralized with e.g. Na2CO3 or NaOH to obtain the corresponding sodium salts, and they are mixed with at least a second surfactant, for example based on polyalkoxylates, such as TSP-(PO)35-(EO)20-SO4NH4. The first option is to transport the acidic ABS composition (M+ = H+) from the manufacturing site to the reservoir location or a location nearby and to carry the neutralization step and, if necessary, to mix it with a second or further surfactants there. For this option to be successful and efficient, it is desired that acidic ABS composition are easy to transport and to handle. This is tested in col. 3 and 4 in Table 1 and discussed below. The second option is to deliver a surfactant concentrated blend with high active content comprising the neutralized ABS and, if necessary, a second or further surfactants directly to the reservoir location or a location nearby. Then the surfactant concentrated blend can be dissolved there to obtain the ready-for-use EOR composition. For this option to be successful and efficient, it is desired that the concentrated blend has the best possible transportation and handling properties. In other words, it is highly desired that the concentrated blend is flowable at 20°C (pour point <20°C) and the viscosity at e.g. 65°C shall be low enough to enable a smooth pumping of the material (sulfated surfactants are stable to at least 60 - 65°C, depending on the pH). This is tested in col. 6 and 7 in Table 1 and discussed below. Furthermore, the suitability of the inventive EOR composition in EOR operations for successfully recovering crude oil. For this, the EOR compositions shall have a clear appearance and be homogeneous and stable. As cloudy solution might lead to plugging of the porous reservoir. And it is highly desired that the addition of the EOR composition into the subterranean formation leads to a Winsor type III emulsion which achieves an ultralow IFT between water and oil (i.e. < 0.01 mN / m). This is tested in col. 8 and 9 in Table 1 and discussed below. First option – transportation of individual components:Column 3 in Table 1 shows that the acidic ABS compositions (M+ = H+) with high active content of the present invention are liquid and low viscous at room temperature. The tested compositions have an active content higher than 90 wt.% and they show a viscosity well under 5000 mPas at 25 ºC and 10 s-1. This demonstrates that acid ABS compositions with high active content can be transported to other locations (e.g. remote reservoir) in an efficient manner, in other words, the transportation of these ABS compositions to other locations (e.g. remote reservoir) requires less storage capacity (e.g. less trucks) and thus less energy than transporting a diluted aqueous neutralized ABS solution (e.g. M+ = Na+) with ca. 10 – 20 wt.% active material.  Once the ABS composition (M+ = H+) has arrived to a near location from the reservoir, the acidic ABS composition shall be neutralized, e.g. with a base such as Na2CO3 or NaOH to obtain the corresponding sodium salt, prior to its introduction into the subterranean well formation. It is important to note that many oil and gas recovery operations are carried out in winter or in locations with very low ambient temperatures. To facilitate the handling of the acidic ABS composition and its neutralization step and to reduce the heating requirements, it is highly desired that the acid ABS composition can still be flowable and pumpable at very low temperatures, i.e. low pour point. Column 4 in Table 1 clearly shows that the inventive ABS composition has a much lower pour point than the comparative composition. The inventive examples 2, 5, 6 and 7 show a pour point of between -30 ºC and -33 ºC, while comparative examples show pour points as high as -9 ºC (C1). Second option – transportation of the surfactant concentrated blend:If the surfactant concentrated blend is delivered directedly to the reservoir location or a location nearby, it is desired that the concentrated blend has a low water content, a high active content and is flowable at 20°C (pour point <20°C), to reduce energy costs for transportation and storage of such a blend. In addition, it is desired that the viscosity at e.g. 65°C is low enough to enable a smooth pumping of the material.  To obtain high active content and low water content, the alkylbenzene sulfonic acids were neutralized with 50 wt% NaOH in water in the presence of the previously described TSP-(PO)35-(EO)20-SO4NH4.  As shown col. 6 and 7 in Table 1, the inventive concentrated blends have the desired pour point of <20°C and a viscosity of around 1000 - 650 mPas at 65°C. That means, that the material is nicely pumpable. In contrast to this, the comparative examples C1 and C4 show that an unwanted waxy material with pour points of >40°C are obtained. In these cases also an unwanted foam formation was observed (due to release of some ammonia) and higher amounts of NaOH solution was needed to achieve the full neutralization of the alkyl benzene sulfonic acid. Suitability of the EOR composition for EOR applications: The solubility of the neutralized alkyl benzene sulfonic acids combined with TSP-(PO)35-(EO)20-SO4NH4 in presence of Na2CO3 at 65°C was investigated. Col. 8 in Table 1 shows the appearance of the aqueous surfactant solution (i.e. EOR composition) at 65°C. All examples show a clear, stable and homogeneous solution, i.e. sufficient solubility was obtained, except for comparative example 3. “Group B” ABS compounds without presence of “group A” ABS compounds are not soluble enough, and thus a cloudy solution is formed. This is highly undesired in crude oil recovery operations because cloudy solutions might lead to plugging of the porous reservoir. Cloudy solutions shall be avoided.  The interaction with a crude oil was investigated. In these tests, a brine having a lower amount of Na2CO3 was selected, so that solubility and optimum phase behaviour match. It is desired that the addition of the EOR composition into the subterranean formation leads to a Winsor type III emulsion which achieves an ultralow IFT between water and oil (i.e. < 0.01 mN / m). The formation of Winsor Type III microemulsions are indicated by formation of golden streaks when crude oil is mixed with aqueous surfactant solution at optimum conditions. Once the Winsor Type III microemulsion was obtained, the SP* was measured and the interfacial tension was calculated using the Huh equation. Col. 9 in Table 1 shows that the inventive EOR compositions successfully achieve ultralow interfacial tensions of <0.01 mN / m.  Comparative example C1 did not lead to a Winsor Type III microemulsion and only a higher IFT was obtained. EOR composition of comparative example 3 (C3) was not tested as it did not provide sufficient solubility. Therefore, the experimental results in Table 1 show that inventive examples 2, 5, 6 and 7 provide the desired match between handling (low pour points and low viscosities), solubility and interfacial tension against crude oil. While the comparative examples C1, C3 and C4 the single compounds do not provide the desired profile and fail in at least one aspect. Embodiments of this invention: 1. A composition comprising alkyl benzene sulfonate ABS(I) and ABS(II) (I) (II) wherein R1 and R2 are independently selected from a saturated alkyl group containing from 2 to 13 carbon atoms; R1 and R2 together have a total of 15 carbon atoms;M+ is independently selected from H+, NH4+ or a monovalent cation, preferably a H+, NH4+, Na+ or K+;the molar ratio of ABS(I) : ABS(II) ranges from 10:90 to 30:70;and wherein the composition comprises at least one further alkyl benzene sulfonate molecule selected from ABS(III), ABS(IV), ABS(V) and mixtures thereof, (III) (IV) (V)  whereinM+ is independently selected from a H+, NH4+ or a monovalent cation, preferably a H+, NH4+, Na+ or K+; andthe molar ratio of the alkyl benzene sulfonates [(I)+(II)] : [(III)+(IV)+(V)] ranges from 90:10 to 99.9:0.1;the alkyl benzene sulfonates (I)-(V) together may be referred as ABS mixture “group A”. 2. In a preferred embodiment of the present invention, the composition further comprises other alkyl benzene sulfonate molecules different from ABS mixture “group A”, and the amount of ABS mixture “group A” is at least 50 wt.%, preferably at least 60 wt.%, more preferably at least 70 wt.%, based on the total weight of all alkyl benzene sulfonate molecules present in the composition. 3. In a preferred embodiment of the present invention, the composition comprises at least one further alkyl benzene sulfonate molecule selected from ABS(VI), ABS(VII), ABS(VIII) and mixtures thereof, (VI) (VII) (VIII)  wherein R3 is a saturated alkyl group containing from 14 to 15 carbon atoms; R4, R5, R6, R7, R8 are independently selected from a saturated alkyl group containing at least 2 carbon atoms;the sum of all carbon atoms in R4 and R5 ranges from 10 to 20 carbon atoms, but none of the single alkyl groups comprises more than 15 carbon atoms; the sum of all carbon atoms in R6, R7 and R8 ranges from 10 to 20 carbon atoms but none of the single alkyl groups comprises more than 15 carbon atoms; M+ is independently selected from a H+, NH4+ or a monovalent cation, preferably a H+, NH4+, Na+ or K+;the alkyl benzene sulfonates (VI)-(VIII) together may be referred as ABS mixture “group B”; andwherein the weight ratio of the ABS mixture “group A” : “group B” ranges from 95:5 to 70:30, preferably 90:10 to 70:30, more preferably 85:15 to 75:25. 4. In a preferred embodiment of the present invention, the molar ration of the alkyl benzene sulfonates (VI) : [(VII)+(VIII)] ranges from 0:100 to 20:80.  5. In a preferred embodiment of the present invention, the composition comprises ABS(IX)(IX) whereinR9 is a saturated alkyl group containing 10 to 13 carbon atoms; M+ is a H+, NH4+ or a monovalent cation, preferably a H+, NH4+, Na+ or K+; andthe alkyl benzene sulfonates (IX) may be referred as ABS mixture “group C”, and the weight ratio ABS mixture “group A”:”group C” ranges from 25 : 75 to 97.5 : 2.5, preferably from 50 : 50 to 97.5 : 2.5, more preferably from 70 : 30 to 95 : 5, and even more preferable from 85 : 15 to 95: 5.  6. In a preferred embodiment of the present invention, the composition further comprises ABS mixture “group C” as defined above wherein the weight ratio of ABS mixture (“group A”+ “group B”) : “group C” ranges from 80:20 to 97.5:2.5, preferably 85:15 to 97.5:2.5, more preferably 85:15 to 95:5. 7. In a preferred embodiment of the present invention, the ABS(IX) are selected from ABS(X) and ABS(XI) (X) (XI)  wherein R10 is a saturated alkyl group containing 8 to 11 carbon atoms,R11 and R12 are independently selected from a saturated alkyl group containing 2 to 10 carbon atoms, R11 and R12 together have a total of 9 to 12 carbon atoms;M+ is independently selected from H+, NH4+ or a monovalent cation; preferably a H+, NH4+, Na+ or K+, andthe weight ratio of ABS(X) : ABS(XI) ranges from 10:90 to 25:75, preferably 14:86 to 21:79. 8. In a preferred embodiment of the present invention, any one of the alkyl chains in ABS (I) – (V) and (IX) – (XI) is at least 90wt.% linear, preferably at least 95 wt.% linear. 9. A concentrated blend comprising an ABS composition according to any of embodiments above-mentioned, a basic ionic salt and a second surfactant, different from any of the ABS (I) – (XI).  10. In a preferred embodiment of the present invention, the second surfactant in the concentrated blend is a polyalkoxylate-based surfactant, preferably a tristyrylphenol alkoxy sulfate surfactant, more preferably TSP-(PO)35-(EO)20-SO4NH4. 11. In a preferred embodiment of the present invention, the weight ratio of the second surfactant to the ABS composition in acidic form in the concentrated blend is between 1:1 to 2:1, preferably 1.4:1 to 1.6:1. 12. An EOR composition comprising an ABS composition according to any of the embodiments above-mentioned, a basic ionic salt and an additional surfactant, different from any of the ABS (I) – (XI), wherein total amount of all surfactants present in the EOR composition is between 0.05 to 2 wt.%, in respect of the total weight of the EOR composition. 13. Use of an EOR composition according to the above-mentioned embodiment in in an oilfield or enhanced oil recovery (EOR) application. 14. In a preferred embodiment of the present invention, the oilfield or EOR application is selected from the group consisting of an EOR surfactant, flow back improver, wetting agent, dispersant, emulsifying agent, drilling fluid, fracturing fluid, spacer fluid, drill cutting cleaner, well bore cleaner and foamer for drilling fluids. 15. A process for recovering oil from an oil-bearing subterranean formation comprising injecting an EOR composition according the above-mentioned embodiment into one or more injection wells, forming a Winsor type III microemulsion, achieving an interfacial tension between crude oil and aqueous surfactant solution of <0.1 mN / m and producing oil from one or more producing wells. 16. In a preferred embodiment of the present invention, the oil bearing subterranean formation contains sandstone or carbonate reservoirs with reservoir temperatures from 15 to 130°C.

Claims

1. A composition comprising alkyl benzene sulfonate ABS(I) and ABS(II) (I) (II) wherein R1 and R2 are independently selected from a saturated alkyl group containing from 2 to 13 carbon atoms; R1 and R2 together have a total of 15 carbon atoms;M+ is independently selected from H+, NH4+ or a monovalent cation, preferably a H+, NH4+, Na+ or K+;the molar ratio of ABS(I) : ABS(II) ranges from 13:87 to 27:73. wherein the composition comprises at least one further alkyl benzene sulfonate molecule selected from ABS(III), ABS(IV), ABS(V) and mixtures thereof, (III) (IV) (V)  whereinM+ is independently selected from a H+, NH4+ or a monovalent cation, preferably a H+, NH4+, Na+ or K+; andthe molar ratio of the alkyl benzene sulfonates [(I)+(II)] : [(III)+(IV)+(V)] ranges from 90:10 to 99.9:0.1;the alkyl benzene sulfonates (I)-(V) together may be referred as ABS mixture “group A”. 2. The composition according to claim 1, wherein the composition further comprises other alkyl benzene sulfonate molecules different from ABS mixture “group A”, and the amount of ABS mixture “group A” is at least 50 wt.%, preferably at least 60 wt.%, more preferably at least 70 wt.%, based on the total weight of all alkyl benzene sulfonate molecules present in the composition. 3. The composition according to claim 1 or 2, wherein the composition comprises at least one further alkyl benzene sulfonate molecule selected from ABS(VI), ABS(VII), ABS(VIII) and mixtures thereof, (VI) (VII) (VIII)  wherein R3 is a saturated alkyl group containing from 14 to 15 carbon atoms; R4, R5, R6, R7, R8 are independently selected from a saturated alkyl group containing at least 2 carbon atoms;the sum of all carbon atoms in R4 and R5 ranges from 10 to 20 carbon atoms, but none of the single alkyl groups comprises more than 15 carbon atoms; the sum of all carbon atoms in R6, R7 and R8 ranges from 10 to 20 carbon atoms but none of the single alkyl groups comprises more than 15 carbon atoms; M+ is independently selected from a H+, NH4+ or a monovalent cation, preferably a H+, NH4+, Na+ or K+;the alkyl benzene sulfonates (VI)-(VIII) together may be referred as ABS mixture “group B”; andwherein the weight ratio of the ABS mixture “group A” : “group B” ranges from 95:5 to 70:30, preferably 90:10 to 70:30, more preferably 85:15 to 75:25. 4. The composition according to claim 3, wherein the molar ration of the alkyl benzene sulfonates (VI) : [(VII)+(VIII)] ranges from 0:100 to 20:

80.  5. The composition according to any one of claims 1 to 4, wherein the composition comprises ABS(IX)(IX) whereinR9 is a saturated alkyl group containing 10 to 13 carbon atoms; M+ is a H+, NH4+ or a monovalent cation, preferably a H+, NH4+, Na+ or K+; andthe alkyl benzene sulfonates (IX) may be referred as ABS mixture “group C”, and the weight ratio ABS mixture (“group A”+ “group B”) : “group C” ranges from 80:20 to 97.5:2.5, preferably 85:15 to 97.5:2.5, more preferably 85:15 to 95:5. 6. The composition according to claim 5, wherein the ABS(IX) are selected from ABS(X) and ABS(XI) (X) (XI)  wherein R10 is a saturated alkyl group containing 8 to 11 carbon atoms,R11 and R12 are independently selected from a saturated alkyl group containing 2 to 10 carbon atoms, R11 and R12 together have a total of 9 to 12 carbon atoms;M+ is independently selected from H+, NH4+ or a monovalent cation; preferably a H+, NH4+, Na+ or K+, andthe weight ratio of ABS(X) : ABS(XI) ranges from 10:90 to 25:75, preferably 14:86 to 21:79. 7. The composition according to any one of the previous claims, wherein any one of the alkyl chains in ABS (I) – (V) and (IX) – (XI) is at least 90% linear. 8. The composition according to any one of the previous claims, wherein the composition additionally comprises a basic ionic salt and a second surfactant.  9. The composition according to claim 8, wherein the second surfactant is a polyalkoxylate-based surfactant, preferably a tristyrylphenol alkoxy sulfate surfactant, more preferably TSP-(PO)35-(EO)20-SO4NH4. 10. The composition according to any one of claims 8 or 9, wherein the weight ratio of the second surfactant to the ABS composition in acidic form is between 1:1 to 2:1, preferably 1.4:1 to 1.6:1. 11. An EOR composition comprising an ABS composition according to any of claims 1 to 7, a basic ionic salt and an additional surfactant, different from any of the ABS (I) – (XI) as described in any one of the claims 1 to 7, wherein the total amount of all surfactants present in the EOR composition is between 0.05 to 2 wt.%, in respect of the total weight of the EOR composition. 12. Use of an EOR composition according to claim 11 in an oilfield or enhanced oil recovery (EOR) application. 13. Use according to claim 12, wherein the oilfield or EOR application is selected from the group consisting of an EOR surfactant, flow back improver, wetting agent, dispersant, emulsifying agent, drilling fluid, fracturing fluid, spacer fluid, drill cutting cleaner, well bore cleaner and foamer for drilling fluids. 14. A process for recovering oil from an oil-bearing subterranean formation comprising injecting a composition according to claim 10 into one or more injection wells, forming a Winsor type III microemulsion, achieving an interfacial tension between crude oil and aqueous surfactant solution of <0.1 mN / m and producing oil from one or more producing wells. 15. The process for recovering oil according to claim 14, wherein the oil bearing subterranean formation contains sandstone or carbonate reservoirs with reservoir temperatures from 15 to 130°C.

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