EP2771426A1 - Procédé d'extraction de pétrole à l'aide de tensioactifs à base d'un mélange d'alcoxylates d'hydrocarbures contenant du guerbet en c28, guerbet en c30, guerbet en c32 - Google Patents

Procédé d'extraction de pétrole à l'aide de tensioactifs à base d'un mélange d'alcoxylates d'hydrocarbures contenant du guerbet en c28, guerbet en c30, guerbet en c32

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Publication number
EP2771426A1
EP2771426A1 EP12772991.1A EP12772991A EP2771426A1 EP 2771426 A1 EP2771426 A1 EP 2771426A1 EP 12772991 A EP12772991 A EP 12772991A EP 2771426 A1 EP2771426 A1 EP 2771426A1
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EP
European Patent Office
Prior art keywords
surfactant
carbon atoms
surfactants
oil
mixture according
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Application number
EP12772991.1A
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German (de)
English (en)
Inventor
Christian Bittner
Günter OETTER
Jack Tinsley
Chistian SPINDLER
Gabriela ALVAREZ JÜRGENSON
Sophie Maitro-Vogel
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BASF SE
Original Assignee
BASF SE
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Publication date
Application filed by BASF SE filed Critical BASF SE
Priority to EP12772991.1A priority Critical patent/EP2771426A1/fr
Publication of EP2771426A1 publication Critical patent/EP2771426A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
    • C09K—MATERIALS FOR MISCELLANEOUS APPLICATIONS, NOT PROVIDED FOR ELSEWHERE
    • C09K8/00—Compositions for drilling of boreholes or wells; Compositions for treating boreholes or wells, e.g. for completion or for remedial operations
    • C09K8/58—Compositions for enhanced recovery methods for obtaining hydrocarbons, i.e. for improving the mobility of the oil, e.g. displacing fluids
    • C09K8/584—Compositions for enhanced recovery methods for obtaining hydrocarbons, i.e. for improving the mobility of the oil, e.g. displacing fluids characterised by the use of specific surfactants

Definitions

  • the present invention relates to a surfactant mixture, its use and preparation, and to aqueous surfactant formulations containing mixtures and methods for producing oil by means of Winsor Type III microemulsion flooding, in which the aqueous surfactant formulation is injected through injection wells into a crude oil deposit and crude oil is removed from the deposit through production wells ,
  • a deposit In natural oil deposits, petroleum is present in the cavities of porous reservoirs, which are closed to the earth's surface by impermeable cover layers.
  • the cavities may be very fine cavities, capillaries, pores or the like. Fine pore necks, for example, have a diameter of only about 1 ⁇ .
  • a deposit In addition to crude oil, including natural gas, a deposit contains more or less saline water.
  • Oil production generally distinguishes between primary, secondary and tertiary production.
  • primary production after drilling the deposit, petroleum automatically streams through the borehole due to the inherent pressure of the deposit.
  • the secondary funding is used.
  • additional wells will be drilled into the oil-bearing formation in addition to the wells that serve to extract the oil, known as production wells.
  • injection wells water is injected into the reservoir to maintain or increase pressure.
  • the oil is slowly forced through the cavities into the formation, starting from the injection well, toward the production well.
  • this only works as long as the cavities are completely filled with oil and the viscous oil is pushed through the water in front of it.
  • the low-viscosity water breaks through cavities, it flows from this point on the path of least resistance, ie through the channel formed, and no longer pushes the oil in front of him.
  • Tertiary oil extraction includes heat processes in which hot water or superheated steam is injected into the reservoir
  • the flooding medium can also be gases such as CO 2 or nitrogen.
  • Tertiary oil production further includes processes in which suitable chemicals are used as auxiliaries for oil extraction. With these, the situation can be influenced towards the end of the flood and thus also promote oil that was previously held in the rock formation.
  • Viscous and capillary forces act on the oil, which is trapped in the pores of the reservoir rock towards the end of the secondary production, and the ratio of these two forces to one another determines the microscopic oil removal.
  • capillary number By means of a dimensionless parameter, the so-called capillary number, the influence of these forces is described. It is the ratio of the viscosity forces (velocity x viscosity of the oppressive phase) to the capillary forces (interfacial tension between oil and water x wetting of the rock):
  • ⁇ is the viscosity of the oil mobilizing fluid
  • v the Darcy velocity (flow per unit area)
  • ⁇ the interfacial tension between petroleum mobilizing liquid and petroleum
  • ⁇ the contact angle between petroleum and rock
  • the capillary number " is 6, and that it is necessary for the capillary to about 10" near the end of secondary oil recovery in the range of about 10 to increase from 3 to 10 "2 to mobilize additional mineral oil.
  • Winsor Type III microemulsion flooding the injected surfactants are expected to form a microemulsion Windsor Type III with the water and oil phases present in the deposit I is not an emulsion with very small droplets, but a thermodynamically stable, liquid mixture of water, oil and surfactants.
  • Their three advantages are that it achieves a very low interfacial tension ⁇ between oil and aqueous phase
  • the microemulsion Winsor Type III is in equilibrium with excess water and excess oil. Under these conditions, the microemulsion formation, the surfactants demonstrate the oil-water interface and lower the interfacial tension ⁇ values of ⁇ 10 "2 mN / m (ultralow interfacial surfactant-sion) are particularly preferred in. In order to achieve an optimum result, the proportion should the Microemulsion in the system Water-microemulsion oil naturally should be as large as possible at a defined amount of surfactant, since in this way the lower interfacial tensions can be achieved.
  • the shape of the oil droplets can be changed (interfacial tension between oil and water is lowered so far that the state of the smallest boundary surface is no longer sought and the spherical shape is no longer preferred) and by the flood water through the capillary openings squeeze through.
  • Winsor Type III microemulsion will be formed if there is an excess amount of surfactant. It thus represents a reservoir for surfactants, which accomplish a very low interfacial tension between oil and water phase.
  • surfactants which accomplish a very low interfacial tension between oil and water phase.
  • the surfactant from the microemulsion can significantly lower the interfacial tension of this new interface and result in mobilization of the oil (for example by deformation of the oil droplets) ,
  • the oil droplets can then combine to form a continuous oil bank. This has two advantages: Firstly, as the continuous oil bank progresses through new porous rock, the oil droplets located there merge with the bank.
  • the union of the oil droplets to an oil bank significantly reduces the oil-water interface, thus releasing unneeded surfactant.
  • the released surfactant may thereafter mobilize residual oil remaining in the formation as described above.
  • Winsor Type III microemulsion flooding is an extremely efficient process and unlike an emulsion flooding process, it requires significantly less surfactant.
  • the surfactants are usually optionally injected together with cosolvents and / or basic salts (optionally in the presence of chelating agents). Subsequently, a solution of thickening polymer is injected for mobility control.
  • Another variant is the injection of a mixture of thickening polymer and surfactants, cosolvents and / or basic see salts (optionally with chelating agent) and subsequently a solution of thickening polymer for mobility control. These solutions should usually be clear to avoid blockage of the reservoir.
  • Suitable surfactants for tertiary oil production are the interfacial tension between water and oil (usually approx. 20 mN / m) to particularly low values of less than 10 "2 mN / m to allow adequate oil mobilization at normal storage temperatures of about 15 ° C to 130 ° C and in the presence of high salty water, especially in the presence of high levels of calcium and / or magnesium ions, the surfactants must therefore also be soluble in strongly saline deposit water.
  • No. 7,119,125 B1 describes a mixture of sulfated Guerbet alcohol alkoxylate and low molecular weight sulfated alkyl alkoxylate in oil production.
  • the bimodal distribution is assigned particularly good emulsifying properties.
  • these emulsifying properties do not play a major role in Winsor type III microemulsion flooding. It would take too much surfactant for the emulsification of oil and the required shear forces are hardly in the flood process before (except for the area around the injector).
  • US-A 2008/217064 describes a Bohr complicatlays containing a nonionic surfactant - consisting of at least one branched alkyl ethoxylate and an end-capped alkyl ethoxylate - and a detergency builder and a thickener.
  • the nonionic surfactant may be a C10 Guerbet alcohol ethoxylate.
  • US-A 2009/270281 describes the use of a surfactant mixture for petroleum production, which contains at least one surfactant having an alkyl radical of 12 to 30 carbon atoms and a branched cosurfactant having an alkyl radical of 6 to 1 1 carbon atoms.
  • the degree of branching of the alkyl radical in the cosurfactant ranges from 1 to 2.5 and may thus include Guerbet alcohols of the type 2-ethylhexyl or 2-propylheptyl.
  • the cosurfactants may be alcohol ethoxylates or anionic modified alcohol ethoxylates (for example, alkyl ether sulfate).
  • the use parameters such as type, concentration and the mixing ratio of the surfactants used are therefore adapted by the skilled person to the conditions prevailing in a given oil formation conditions (for example, temperature and salinity).
  • the oil production is proportional to the capillary number. This is the higher the lower the interfacial tension between oil and water. Low interfacial tensions are the more difficult to achieve the higher the average number of carbon atoms in the crude oil.
  • surfactants are suitable which have a long alkyl radical. The longer the alkyl radical, the better the interfacial tensions can be reduced.
  • the availability of such compounds is very limited.
  • a further object of the invention is to provide a process for the preparation of these surfactants or surfactant mixtures.
  • the object is achieved by a surfactant mixture containing, with respect to the hydrocarbon moiety (R 1 ) (R 2 ) -CH-CH 2 - at least three different ionic surfactants of the general formula (I)
  • R 1 is a linear or branched, saturated or unsaturated aliphatic hydrocarbon radical having 12 to 14 carbon atoms;
  • R 2 is a linear or branched, saturated or unsaturated aliphatic
  • Hydrocarbon radical having 14 to 16 carbon atoms
  • each A ° is independently ethylene, propylene (preferably 1, 2-propylene) or butylene (preferably 1, 2-butylene);
  • k is an integer from 1 to 99
  • X is a branched or unbranched alkylene group having 1 to 10 carbon atoms which may be substituted with an OH group;
  • Y a represents a sulfate group, sulfonate group, carboxylate group or a phosphate group (preferably a sulfate or carboxylate group, more preferably a sulfate group);
  • b is 1, 2 or 3 (preferably 1) and
  • a is 1 or 2 (preferably 1).
  • a further aspect of the present invention relates to an aqueous surfactant formulation containing a surfactant mixture according to the invention, wherein preferably the surfactant formulation has a total surfactant content of from 0.05 to 5% by weight with respect to the total amount of the aqueous surfactant formulation.
  • a further aspect of the present invention relates to the use of a surfactant mixture according to the invention or of a surfactant formulation according to the invention in crude oil production, by means of Winsor Type III microemulsion flooding.
  • Another aspect of the present invention relates to methods for oil production, by means of Winsor Type III microemulsion flooding, in which an aqueous surfactant formulation according to the invention for the purpose of lowering the interfacial tension between oil and water to ⁇ 0.1 mN / m, injected through at least one injection well into a Erdöllager GmbH and the Deposit is taken through at least one production well of crude oil.
  • a blend of at least 3 different ionic surfactants with respect to the hydrocarbon moiety (R 1 ) (R 2 ) -CH-CH 2 and a tertiary petroleum recovery process using Winsor Type III microemulsion flooding, comprising an aqueous surfactant formulation comprising hydrocarbons - Hydrogen part (R 1 ) (R 2 ) -CH-CH 2 - at least three different ionic surfactants is injected through at least one injection well in a Erdöllager GmbH, the interfacial tension between oil and water on values ⁇ 0.1 mN / m, preferably to values ⁇ 0.05 mN / m, more preferably values ⁇ 0.01 mN / m is lowered, and the reservoir is withdrawn through at least one production well crude oil.
  • R 1 is a linear or branched, saturated or unsaturated aliphatic hydrocarbon radical having 12 or 14 carbon atoms and R 2 is a linear or branched, saturated or unsaturated aliphatic hydrocarbon radical having 14 or 16 carbon atoms.
  • R 1 is a linear, saturated or unsaturated (preferably saturated) aliphatic hydrocarbon radical having 12 or 14 carbon atoms and R 2 is a linear, saturated or unsaturated (preferably saturated) aliphatic hydrocarbon radical having 14 or 16 carbon atoms , and in particular by at least 3 ionic surfactants of the general formula (I) having a hydrocarbon radical having 28 carbon atoms, 30 carbon atoms and 32 carbon atoms.
  • the C 2 8 surfactant of the general formula (I) is particularly preferably in a range from 40% to 60%, and the C 30 surfactant of the general formula (I) in one range from 30% to 50% and the C 32 surfactant of the general formula (I) in a range of 1% to 20% based on the total. It is further preferred that the proportion by weight of the three ionic surfactants based on the total weight of the surfactant mixture according to the invention is greater than 50% by weight, more preferably greater than 60% by weight, more preferably greater than 70% by weight, even more preferably greater than 80% by weight .-%, more preferably greater than 90 wt .-% is.
  • k is an integer in the range of 4 to 50.
  • the radical (OX) 0 Y a " preferably stands for OS (O) 2 O “ , OCH 2 CH 2 S (O) 2 O “ , OCH 2 CH (OH) CH 2 S (O) 2 0 “ , 0 (CH 2 ) 3 S (0) 2 0 " , S (0) 2 0 “ , CH 2 C (0) 0 " or for CH 2 CH (R ') C (0) 0 " , where R 'is hydrogen or an alkyl radical having 1 to 4 C atoms (for example methyl).
  • alkyleneoxy (AO) groups OA ° in formula (I), which occur k-fold, may be the same or different. If these are different, they can be distributed statistically, alternately or in blocks, ie be arranged in two, three four or more blocks.
  • the n-butylene, m-propylene and ethyleneoxy groups are at least partially (preferably at least 50%, more preferably at least 60%, more preferably at least 70%, more preferably at least 80%, more preferably greater than) at least 90%, in particular completely) arranged in blocks.
  • Arranged in blocks means in the context of the present invention that at least one AO has a neighboring group AO which is chemically identical, so that these form at least two AOs a block.
  • m is an integer from 4 to 15 (more preferably 5 to 9) and / or I is an integer from 0 to 25 (more preferably 4 to 15) and / or n is an integer from 2 to 15 ( more preferably 5 to 9).
  • the invention relates to a mixture of with respect to the hydrocarbon moiety (R 1 ) (R 2 ) -CH-CH 2 - three ionic surfactants and their use, wherein m is a number from 4 to 15, n is a number is from 0 to 15 and Y a "is selected from the group of sulfate groups, sulfonate groups and carboxylate groups, wherein the groups BuO, PO and EO more than 80% in block form in the order BuO, PO, EO starting from (R 1 ) (R 2 ) -CH-CH 2 , and the sum I + m + n ranges from 5 to 49.
  • a particularly preferred embodiment is where n is a number from 2 to 15, m is one Number of 5 to 9, and Y a "is selected from the group of sulfate groups, sulfonate groups and carboxylate groups, wherein the groups A and B more than 80% in block form in the order BuO, PO and EO starting from (R 1 ) (R 2 ) -CH-CH 2 , the sum of I + m + n ranges from 4 to 50 and the block BuO consists of more than 80% 1, 2-butylene oxide.
  • a preferred surfactant mixture according to the invention also contains surfactants of the formula
  • R 1 is a linear, saturated aliphatic hydrocarbon radical having 12 or 14 carbon atoms and in the general formula (III) R 2 is a linear, saturated aliphatic hydrocarbon radical with 14 or 16 carbon atoms.
  • an aqueous surfactant formulation which, with respect to the hydrocarbon moiety (R 1 ) (R 2 ) -CH-CH 2 -, has at least three different surfactants of the general formula Contains (I). It may also include other surfactants and / or other components.
  • the interfacial tension between oil and water is by the use of the surfactant mixture to values ⁇ 0.1 mN / m, preferably to ⁇ 0.05 mN / m, particularly preferably Lowered ⁇ 0.01 mN / m.
  • the interfacial tension between oil and water becomes values in the range of 0.1 mN / m to 0.0001 mN / m, preferably values in the range of 0.05 mN / m to 0.0001 mN / m, more preferably lowered to values in the range of 0.01 mN / m to 0.0001 mN / m.
  • the three different surfactants with respect to the hydrocarbon moiety (R 1 ) (R 2 ) -CH-CH 2 can be subsumed under the general formula (I). The difference may be due to the number of carbon atoms, the number of unsaturated bonds, the branching frequency and / or the degree of branching. In particular, the surfactants differ in chain length, which is given for R 1 and R 2 .
  • R 1 / R 2 hydrocarbon chains with 12/14, 12/15, 12/16, 13/14, 13/15, 13/16, 14/14, 14/15, 14/16, preferably 12/14 , 12/16, 14/14, 14/16 carbon atoms.
  • the three surfactants with respect to the hydrocarbon moiety (R 1 ) (R 2 ) -CH-CH 2 - with 28, 30 and 32 carbon atoms preferably form the main components of the surfactant mixture according to the invention. Their proportion is preferably at least 25 wt .-% based on the total weight of the surfactant mixture, more preferably at least 30 wt .-%, more preferably at least 40 wt .-%, more preferably at least 50% by weight.
  • the radical R 1 is a linear or branched, saturated or unsaturated aliphatic hydrocarbon radical having 12 to 14 carbon atoms.
  • the radical R 2 is a linear or branched, saturated or unsaturated aliphatic hydrocarbon radical having 14 to 16 carbon atoms.
  • R 1 is either identical to R 2 or preferably has at most two C atoms (more preferably exactly two C atoms) less than R 2 .
  • the degree of branching in R 1 or R 2 is preferably in the range from 0.1 to 5 (preferably from 0.1 to 1.5).
  • the degree of branching in R 1 or R 2 is preferably in the range from 0.1 to 5 (preferably from 0.1 to 1.5).
  • degree of branching is hereby defined in a manner known in principle as the number of methyl groups in a molecule of the alcohol minus 1.
  • the mean degree of branching is the statistical average of the degrees of branching of all molecules in a sample.
  • a preferred embodiment is the use of linear saturated or unsaturated radicals R 1 having 12 or 14 carbon atoms or R 2 having 14 or 16 carbon atoms. Particularly preferred is the use of linear saturated radicals R 1 and R 2 . This results in a degree of branching of 1 for the aliphatic hydrocarbon radical (R 1 ) (R 2 ) -CHCH 2 .
  • I, m and n stand for natural numbers including 0, ie 0, 1, 2, etc.
  • this definition is the definition of a single surfactant.
  • the numbers I and m are average values over all molecules of the surfactants, since in the alkoxylation of alcohol with ethylene oxide or propylene oxide or butylene oxide each have a certain distribution of chain lengths. This distribution can be described in a manner known in principle by the so-called polydispersity D.
  • D M w / M n is the quotient of the weight average molar mass and the number average molar mass.
  • the polydispersity can be determined by means of the methods known to the person skilled in the art, for example by means of gel permeation chromatography.
  • I is a number from 0 to 99, preferably 1 to 40, particularly preferably 1 to 20.
  • m is a number from 0 to 99, preferably 1 to 20, particularly preferably 4 to 15.
  • n is a number from 0 to 99, preferably 1 to 20, more preferably 2 to 15.
  • X is a branched or unbranched alkylene group having 1 to 10, preferably 2 to 4, carbon atoms which may be substituted with an OH group.
  • the alkylene group is preferably a methylene, ethylene or propylene group.
  • X 2 is preferably CH 2 CH 2 , CH 2 CH (OH) CH 2 , (CH 2 ) 3, CH 2 or CH 2 CH (R '), where R' is hydrogen or an alkyl radical having 1 to 4 C atoms ( for example, methyl).
  • Y a represents a sulphonate, sulphate, carboxylate or phosphate group (preferably sulphonate, sulphate or carboxylate group, in particular sulphate and carboxylate)
  • a can stand for values 1 or 2.
  • M + is a cation, preferably a cation selected from the group Na + ; K ⁇ Li ⁇ NH 4 + , H + , Mg 2+ and Ca 2+ (preferably Na + , K + or NH 4 + ).
  • Altogether b can stand for values 1, 2 or 3.
  • the alcohols (R 1 ) (R 2 ) -CH-CH 2 -OH which can serve as starting compound for the preparation of the surfactants of the invention are, for example, by the dimerization of alcohols of the type R 1 CH 2 CH 2 OH and R 2 OH accessible with elimination of water.
  • a further aspect of the present invention is a process for preparing a surfactant mixture according to the invention comprising the steps:
  • step (c) reaction of the alcohol alkoxylates obtained in step (b) with a group Y a " , if appropriate with formation of a spacer group OX.
  • the dimerization of the alcohols of the formula R-CH 2 CH 2 -OH may be a mixture of alcohols.
  • This can include a C14C16 fatty alcohol mixture (linear, saturated), a C14C16 mixture of Ziegleralkoholen 14 and 16 carbon atoms, a C14C16 fatty alcohol mixture (linear and partially unsaturated) or a mixture of C14C16 oxo alcohol.
  • R is a linear saturated or unsaturated (preferably saturated) aliphatic hydrocarbon radical having 12 or 14 carbon atoms.
  • mixtures of the alcohols (II) are condensed.
  • the condensation of alcohols (II) to Guerbet alcohols is preferably carried out in the presence of from 0.5 to 10% by weight, based on the alcohol, of alkali metal or alkaline earth metal hydroxide, for example lithium hydroxide, sodium hydroxide, cesium hydroxide or potassium hydroxide, preferably potassium hydroxide.
  • alkali metal or alkaline earth metal hydroxide are used in a concentration of 3 to 6% by weight, based on the alcohol.
  • the alkali or alkaline earth metal hydroxide can be used in solid form (flakes, powder) or in the form of a 30 to 70%, preferably 50%, aqueous solution.
  • the alcohols of the formula (II) are condensed in the presence of NaOH and / or KOH.
  • Catalysts or catalysts include those known in the art, such as US Pat. No. 3,398,880 (nickel, lead salts), US Pat. No. 3,555,871 (copper, lead, zinc, chromium, molybdenum, tungsten and maganese oxides), US Pat 3979466 (palladium complexes) or still in US 3864407 (silver complexes).
  • ZnO is preferably used as a catalyst for the dimerization.
  • the catalyst or catalysts are preferably ZnO catalysts which are generally added to the mixture from which the Guerbet alcohols are made.
  • the mixture of Guerbet alcohols can be prepared by the process known from DE 3901095 A1.
  • the Guerbet alcohols are synthesized in process step (a) at a temperature in the range from 150 to 320 ° C., preferably at a temperature in the range from 180 to 280 ° C., if appropriate in the presence of a catalyst or catalysts.
  • the surfactants according to the general formula can be prepared in a manner known in principle by alkoxylation of corresponding alcohols (R 1 ) (R 2 ) -CH-CH 2 -OH in process step (b).
  • the implementation of such alkoxylations is known in principle to the person skilled in the art. It is also known to the person skilled in the art that the reaction conditions, in particular the choice of catalyst, can influence the molecular weight distribution of the alkoxylates.
  • the surfactants according to the general formula can preferably be prepared in process step (b) by base-catalyzed alkoxylation.
  • the alcohol (R 1 ) (R 2 ) -CH-CH 2 -OH in a pressure reactor with alkali metal hydroxides, preferably potassium hydroxide, or with alkali metal, such as sodium methylate, are added.
  • alkali metal hydroxides preferably potassium hydroxide, or with alkali metal, such as sodium methylate
  • reduced pressure for example ⁇ 100 mbar
  • temperature 30 to 150 ° C
  • water still present in the mixture can be removed.
  • the alcohol is then present as the corresponding alkoxide.
  • inert gas for example nitrogen
  • the alkylene oxide (s) is added stepwise at temperatures of 60 to 180 ° C. up to a maximum pressure of 10 bar.
  • the alkylene oxide is initially metered in at 130.degree.
  • the temperature rises up to 170 ° C due to the released heat of reaction.
  • the butylene oxide is first added at a temperature in the range of 125 to 145 ° C, then the propylene oxide is added at a temperature in the range of 130 to 145 ° C and then the ethylene oxide at a temperature in the range of 125 to 155 ° C was added.
  • the catalyst can be neutralized, for example by addition of acid (for example acetic acid or phosphoric acid) and filtered off as required.
  • the alkoxylation of the alcohols (R 1 ) (R 2 ) -CH-CH 2 -OH can also be carried out by other methods, for example by acid-catalyzed alkoxylation. tion.
  • DMC catalysts are disclosed, for example, in DE 10243361 A1, in particular in sections [0029] to [0041] and in the literature cited therein.
  • Zn-Co type catalysts can be used.
  • the alcohol (R 1 ) (R 2 ) -CH-CH 2 -OH may be added with the catalyst, the mixture dewatered as described above and reacted with the alkylene oxides as described. It is usually not more than 1000 ppm catalyst used with respect to the mixture and the catalyst may remain in the product due to this small amount.
  • the amount of catalyst can typically be less than 1,000 ppm, for example 250 ppm or less.
  • Process (c) relates to the reaction of the alcohol alkoxylates obtained in step (b) with a group Y a " , if appropriate with the formation of a spacer group OX.
  • sulfate and phosphate groups can be introduced by reacting them directly (optionally after activation) with the alcohol.
  • Sulfonate groups can be introduced by vinyl addition, substitution reaction or aldol reaction, optionally with subsequent hydrogenation, to produce corresponding spacers OX.
  • the alcohol may also be previously converted to a chloride, which is then available for direct sulfonation.
  • a sulphate group it is possible to resort, for example, to the reaction with sulfuric acid, chlorosulphonic acid or sulfur trioxide in the falling film reactor with subsequent neutralization.
  • a sulphonate group for example, the reaction with propanesultone and subsequent neutralization, butansultone and subsequent neutralization, with vinylsulfonic acid sodium salt or with 3-chloro-2-hydroxy-propanesulfonic sodium salt.
  • the terminal OH group can also be converted into a chloride, for example with phosgene or thionyl chloride, and then reacted, for example, with sulfite.
  • carboxylate group it is possible, for example, to oxidize the alcohol with oxygen and subsequent neutralization or the conversion. resort to chloroacetic acid sodium salt.
  • Carboxylates can also be obtained, for example, by Michael addition of (meth) acrylic acid or esters.
  • Phosphates can be obtained, for example, by esterification reaction with phosphoric acid or phosphorus pentachloride.
  • the formulation may additionally optionally comprise further surfactants.
  • surfactants are, for example, anionic surfactants of the type alkylarylsulfonate, petroleum sulfonate or olefinsulfonate (alpha-olefinsulfonate or internal olefinsulfonate) and / or nonionic surfactants of the type alkylethoxylate or alkylpolyglucoside.
  • Betainic surfactants may also be used.
  • These other surfactants may in particular also be oligomeric or polymeric surfactants. With such polymeric cosurfactants, the amount of surfactants necessary to form a microemulsion can be advantageously reduced.
  • polymeric cosurfactants are also referred to as "microemulsion boosters.”
  • polymeric surfactants include amphiphilic block copolymers comprising at least one hydrophilic and at least one hydrophobic block, examples of which include polypropylene oxide-polyethylene oxide block copolymers, polyisobutylene-polyethylene oxide Block copolymers and comb polymers having polyethylene oxide side chains and a hydrophobic main chain, wherein the main chain preferably comprises essentially olefins or (meth) acrylates as building blocks
  • polyethylene oxide is intended to include in each case polyethylene oxide blocks comprising propylene oxide units as defined above , Further details of such surfactants are disclosed in WO 2006/131541 A1.
  • a suitable aqueous formulation of the surfactants according to the general formula is injected into the crude oil deposit through at least one injection well and crude oil is taken from the deposit through at least one production well.
  • crude oil in this context does not mean phase-pure oil, but means the usual crude oil-water emulsions, as a rule, a deposit is provided with several injection wells and several production wells.
  • the main effect of the surfactant lies in the reduction of the interfacial tension between water and oil - desirably to values significantly ⁇ 0.1 mN / m.
  • surfactant flooding or preferably the Winsor type III "microemulsion flooding”
  • water can be injected into the formation to maintain the pressure ("water flooding") or preferably a more viscous aqueous solution of a strongly thickening polymer ("polymer flooding”).
  • water flooding water flooding
  • polymer flooding preferably a more viscous aqueous solution of a strongly thickening polymer
  • Another known technique is the injection of a solution of surfactants and thickening polymers followed by a solution of thickening polymer.
  • the person skilled in the details of the technical implementation of "Tensidflutens", “Wasserflu- tens” and the "polymer flooding” known and he applies depending on the nature of the deposit a corresponding technique.
  • an aqueous formulation which contains surfactants of the general formula (I) is used.
  • the formulations may optionally also contain water-miscible or at least water-dispersible organic or other agents.
  • Such additives are used in particular for stabilizing the surfactant solution during storage or transport to the oil field.
  • the amount of such additional solvents should as a rule not exceed 50% by weight, preferably 20% by weight.
  • only water is used for formulation.
  • water-miscible solvents include, in particular, alcohols, such as methanol, ethanol and propanol, butanol, sec-butanol, pentanol, butyl ethylene glycol, butyl diethylene glycol or butyl triethylene glycol.
  • alcohols such as methanol, ethanol and propanol
  • butanol butanol, sec-butanol
  • pentanol butyl ethylene glycol
  • butyl diethylene glycol or butyl triethylene glycol butyl triethylene glycol.
  • the main component among all Make up surfactants are preferably at least 25% by weight, more preferably at least 30% by weight, very preferably at least 40% by weight and very, very preferably at least 50% by weight of all surfactants used.
  • the mixture used according to the invention can preferably be used for the surfactant flooding of deposits. It is particularly suitable for Winsor type III microemulsion flooding (flooding in the Winsor III area or in the area of existence of the bicontinuous microemulsion phase).
  • Winsor type III microemulsion flooding frlooding in the Winsor III area or in the area of existence of the bicontinuous microemulsion phase.
  • the technique of microemulsion flooding has already been described in detail at the beginning.
  • the formulations may also contain other components, such as, for example, C 4 -C 8 -alcohols and / or basic salts (so-called "alkaline surfactant flooding") .
  • alkaline surfactant flooding for such additives, for example, retention in the formation can be reduced
  • the ratio by weight of the alcohols with respect to the total amount of surfactant used is generally at least 1: 1 - however, a significant excess of alcohol can also be used
  • the amount of basic salts can typically be from 0.1% by weight to 5% by weight. % range basic salts may optionally be added chelating agents (such as EDTA) - typically 0.03% to 5% by weight.
  • the deposits in which the process is used have a temperature of at least 10 ° C, for example 10 to 150 ° C, preferably a temperature of at least 15 ° C to 120 ° C.
  • the total concentration of all surfactants together is 0.05 to 5 wt .-% with respect to the total amount of the aqueous surfactant formulation, preferably 0.1 to 2.5 wt .-%.
  • concentration of surfactants may change upon injection into the formation because the formulation may mix with formation water or absorb surfactants also on solid surfaces of the formation. It is the great advantage of the mixture used according to the invention that the surfactants lead to a particularly good lowering of the interfacial tension.
  • the total concentration of the surfactants in such a concentrate is 10 to 45% by weight.
  • the alkylene oxide is metered in such that the temperature remains between 125 ° C to 155 ° C (for ethylene oxide) and 130 to 145 ° C (for propylene oxide) and 125 to 145 ° C (for 1, 2-butylene oxide).
  • the mixture is then stirred for 5 h at 125 to 145 ° C, rinsed with N 2 , cooled to 70 ° C and the reactor emptied.
  • the basic crude product is neutralized with acetic acid. Alternatively, the neutralization can be carried out with commercially available Mg silicates, which are then filtered off.
  • the bright product is characterized by means of a 1 H-NMR spectrum in CDCl 3, a gel permeation chromatography and an OH number determination, and the yield is determined.
  • the alcohol to be alkoxylated (1, 0 eq) with a double metal cyanide catalyst eg DMC catalyst from BASF type Zn-Co
  • a double metal cyanide catalyst eg DMC catalyst from BASF type Zn-Co
  • the amount of DMC is 0.1% by weight and less of the product to be produced.
  • the mixture is then flushed three times with N 2 , a pre-pressure of about 1.3 bar N 2 is set and the temperature is increased to 120 to 130 ° C.
  • the alkylene oxide is metered in such that the temperature remains between 125 ° C to 135 ° C (for ethylene oxide) and 130 to 140 ° C (for propylene oxide) and 135 to 145 ° C (for 1, 2-butylene oxide).
  • the mixture is then stirred for 5 h at 125 to 145 ° C, rinsed with N 2 , cooled to 70 ° C and the reactor emptied.
  • the bright product is characterized by means of a 1 H NMR spectrum in CDCl 3, a gel permeation chromatography and an OH number determination, and the yield is determined.
  • the alkyl alkoxylate (1, 0 eq) to be sulfated is dissolved in 1.5 times the amount of dichloromethane (on a weight percent basis) and cooled to 5-10 ° C. Thereafter, chlorosulfonic acid (1, 1 eq) is added dropwise so that the temperature does not exceed 10 ° C.
  • the mixture is allowed to warm to room temperature and stir for 4 h at this temperature under N 2 stream, before the above reaction mixture in an aqueous NaOH solution with half volume at max. 15 ° C is dropped.
  • the amount of NaOH is calculated so that there is a slight excess with respect to the chlorosulfonic acid used.
  • the resulting pH is around pH 9-10.
  • lormethan is applied under a slight vacuum on a rotary evaporator at max. 50 ° C away.
  • the product is characterized by 1 H-NMR and the water content of the solution is determined (about 70%).
  • the interfacial tension between water and oil is determined in a known manner via the measurement of the solubilization parameter SP * .
  • the determination of the interfacial tension via the determination of the solubilization parameter SP * is a method accepted in the art for the approximate determination of the interfacial tension.
  • the solubilization parameter SP * indicates how many ml of oil per ml of surfactant used is dissolved in a microemulsion (Windsor type III).
  • the interfacial tension ⁇ can be calculated from the approximate formula IFT "0.3 / (SP * ) 2 if equal volumes of water and oil are used (C. Huh, J. Coli., Interf. Sc, Vol. 71, No. 2 (1979)).
  • the formation of the microemulsion can be visually observed or by means of conductivity measurements. It forms a three-phase system (upper phase oil, middle phase microemulsion, lower phase water). If the upper and lower phases are the same size and no longer change over a period of 24 h, then the optimum temperature (T opt ) of the microemulsion has been found. The volume of the middle phase is determined. From this volume, the volume of added surfactant is subtracted. The value obtained is then divided by two. This volume is now divided by the volume of added surfactant. The result is noted as SP * .
  • the type of oil and water used to determine SP * is determined according to the system under investigation.
  • petroleum itself can be used, or even a model oil such as decane.
  • Both pure water and saline water can be used as water to better model the conditions in the oil formation.
  • the composition of the aqueous phase can be adjusted, for example, according to the composition of a particular reservoir water. Alternatively, an aqueous NaCl solution can also be used.
  • the surfactants are optionally combined and tested with anionic cosurfactants and cosolvents for comparability with known systems.
  • Another possible test form determines the determination of the interfacial tension of crude oil in the presence of the surfactant solution at the appropriate temperature per spinning-drop method on a SVT20 from DataPhysics. For this purpose, an oil drop is injected into a capillary temperature filled with saline surfactant solution and the extent of the drop is observed at approximately 4500 revolutions per minute until a constant value is established. This is usually the case after 2 hours.
  • the interfacial tension IFT (or ⁇ ⁇ ) is calculated hereby - as described by Hans-Dieter Dörfler in "Interfacial and Colloidal Disperse Systems” Springer Verlag Berlin Heidelberg 2002 - according to the following formula from the cylinder diameter d z , the speed ⁇ , and the density difference (drd 2 ):
  • crude oil from a deposit at 20 ° C was used in the present case.
  • the oil has about 16 ° API.
  • the reservoir temperature is about 20 ° C.
  • the reservoir water is salty. With the help of NaCl and NaHC0 3, the salinity was artificially adjusted.
  • a surfactant solution was used which could be injected into the formation.
  • it contained water and salt.
  • the surfactant solution contained a 0.1% of a mixture of alkyl ether sulfates of the Guerbet alkyl 7BuO 7PO 10EO sulfate type and Petrostep S3B (internal olefinsulfonate from Stepan) and 0.05% butyl diethylene glycol and 0.07% Sokalan® PA 20 (polyacrylate sodium salt).
  • the alkyl ether sulfates according to the invention and non-inventive surfactants were used. In the latter case, the examples were marked with "V".
  • the total surfactant concentration and the amount of Na 2 C0 3 are based on the active substance and are given in percent by weight of the aqueous phase.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Emulsifying, Dispersing, Foam-Producing Or Wetting Agents (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

La présente invention concerne un mélange tensioactif contenant par rapport à la fraction d'hydrocarbures (R1)(R2)-CH-CH2- au moins trois tensioactifs ioniques différents de la formule générale (I), dans laquelle R1, R2, A0, k, X, o, Y, a, b, M sont tels que définis dans la description et les revendications. L'invention concerne également l'utilisation et la production dudit mélange ainsi que les formulations de tensioactifs aqueuses contenant ces mélanges, et un procédé d'extraction de pétrole par injection de micro-émulsions Winsor de type III, selon lequel la formulation de tensioactifs aqueuse est injectée par des orifices d'injection dans un gisement pétrolifère et du pétrole brut est prélevé du gisement par des orifices de production.
EP12772991.1A 2011-10-24 2012-10-19 Procédé d'extraction de pétrole à l'aide de tensioactifs à base d'un mélange d'alcoxylates d'hydrocarbures contenant du guerbet en c28, guerbet en c30, guerbet en c32 Withdrawn EP2771426A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP12772991.1A EP2771426A1 (fr) 2011-10-24 2012-10-19 Procédé d'extraction de pétrole à l'aide de tensioactifs à base d'un mélange d'alcoxylates d'hydrocarbures contenant du guerbet en c28, guerbet en c30, guerbet en c32

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP11186289 2011-10-24
PCT/EP2012/070729 WO2013060622A1 (fr) 2011-10-24 2012-10-19 Procédé d'extraction de pétrole à l'aide de tensioactifs à base d'un mélange d'alcoxylates d'hydrocarbures contenant du guerbet en c28, guerbet en c30, guerbet en c32
EP12772991.1A EP2771426A1 (fr) 2011-10-24 2012-10-19 Procédé d'extraction de pétrole à l'aide de tensioactifs à base d'un mélange d'alcoxylates d'hydrocarbures contenant du guerbet en c28, guerbet en c30, guerbet en c32

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EP (1) EP2771426A1 (fr)
JP (1) JP2014534994A (fr)
CN (1) CN103998565A (fr)
CA (1) CA2848961A1 (fr)
EA (1) EA201490776A1 (fr)
IN (1) IN2014CN02832A (fr)
MX (1) MX2014004412A (fr)
WO (1) WO2013060622A1 (fr)

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US9605198B2 (en) 2011-09-15 2017-03-28 Chevron U.S.A. Inc. Mixed carbon length synthesis of primary Guerbet alcohols
US9422469B2 (en) * 2013-03-15 2016-08-23 Chevron U.S.A. Inc. Mixed carbon length synthesis of primary guerbet alcohols

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US3979466A (en) 1973-06-06 1976-09-07 Continental Oil Company Process for condensation of alcohols
US3864407A (en) 1973-06-06 1975-02-04 Continental Oil Co Catalytic Process For Producing Higher Molecular Weight
DE3901095A1 (de) 1989-01-16 1990-07-19 Henkel Kgaa Verfahren zur herstellung von guerbet-alkoholen
DE4325237A1 (de) 1993-07-28 1995-02-02 Basf Ag Verfahren zur Herstellung von Alkoxylierungsprodukten in Gegenwart von mit Additiven modifizierten Mischhydroxiden
DE10243361A1 (de) 2002-09-18 2004-04-01 Basf Ag Alkoxylatgemische und diese enthaltende Waschmittel
US7119125B1 (en) * 2003-09-26 2006-10-10 O'lenick Jr Anthony J Bi-modal Guerbet alkoxy sulfate surfactants
DE102005026716A1 (de) 2005-06-09 2006-12-28 Basf Ag Tensidmischungen für die tertiäre Erdölförderung
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EP2558546A4 (fr) * 2010-04-16 2013-09-18 Univ Texas Tensioactifs alcoxylate d'alcool de guerbet et leur utilisation dans le cadre d'applications de récupération d'huile améliorées
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MX2014004412A (es) 2014-09-11
WO2013060622A1 (fr) 2013-05-02
CN103998565A (zh) 2014-08-20
CA2848961A1 (fr) 2013-05-02
EA201490776A1 (ru) 2014-10-30
JP2014534994A (ja) 2014-12-25
IN2014CN02832A (fr) 2015-07-03

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