Patent Application
20190153298
The present invention relates to zwitterionic surfactants bearing a (sulfo)betaine group that are, inter alia, suitable for enhanced oil recovery (EOR). The invention more specifically relates to specific zwitterionic surfactants, preparation thereof and use in oil recovery from natural oil reservoirs, especially for EOR applications.
In the present description, the generic term “(sulfo)betaine group” refers to a group selected from:
In the instant description, the expression “surfactants bearing a (sulfo)betaine group” intend to encompass any surfactant carrying at least one group betaine and/or sultaine as defined above, and also mixtures of surfactants each of them carrying at least one group betaine and/or sultaine.
Oil recovery from natural oil reservoirs provides the word economy with the necessary fuel and raw materials for a vast number of processes and products.
Generally, three different techniques are used for recovering oil from natural reservoirs.
During primary recovery the natural pressure of the reservoir or gravity drives oil into the well bore, combined with artificial lift techniques such as pumps which bring the oil to the surface. Only about 10% of the oil content of the reservoir are usually produced during primary recovery.
Secondary recovery techniques extend the reservoirs productive life generally by injecting water or gas to displace the oil and drive it to a production wellbore which ultimately results in the recovery of approximately 20 to 40% of the original oil in place.
In view of the fact that much of the easy to produce oil recoverable by primary or secondary recovery has been exploited with leaving on average 60% or more of the original oil remaining in the reservoir, oil producers are interested in enhanced oil recovery techniques which offer the perspective for ultimately exploiting a higher percentage of the original oil content of the oil reservoir. These techniques are summarized in the term Enhanced Oil Recovery (herein referred to as EOR) or tertiary oil recovery.
EOR especially includes methods that is often referred to as “chemical oil recovery” or “chemical EOR” and involves the use of specific chemical compounds or compositions to increase the effectiveness of water floods or the use of detergent-like surfactants to help lower the interfacial tension between the crude oil in the reservoir and the injected brine which often prevents oil droplets from moving through a reservoir.
Whereas in a fresh oil reservoir the oil is present as a continuous phase in the rock formation, this continuous oil phase disintegrates with increasing primary and secondary recovery leaving the oil in discrete droplets which are retained in narrow pores under the effect of high interfacial tension. Overcoming the capillary forces requires either a high pressure or a very considerable reduction in the interfacial tension between water and oil which is targeted through the use of surfactants. The reduction of interfacial tension achievable depends on a variety of different influencing factors such as reservoir temperature, salinity of the reservoir water and composition of the oil itself.
There is an ongoing need in this connection for compositions suitable for enhanced oil recovery which can be fine tuned according to the specific situation in the reservoir in the geological structure as e.g. salinity of the reservoir water, adjustment of interfacial tension and satisfactory solubility in the stream to be injected.
An object of the present invention is to provide zwitterionic surfactants suitable for use in enhanced oil recovery techniques.
To this end, the instant invention proposes specific surfactants, which are obtained via a new process route and that were not known in the prior art to the best knowledge of the inventors.
More precisely, according to a first aspect, one subject-matter of the instant invention is a surfactant of the formula (I):
wherein:
The quaternary ammonium groups of the compounds of formula (I) are associated with counter-anion which may be, in ail or part, the group A in an anionic form and/or, in all or part, counter-anions such as chloride, bromide, or sulfate.
Especially for costs reasons, Ra and Rb are preferably linear groups, typically linear hydrocarbon groups. The surfactants of formula (I) possess, as such, a branched structure of their hydrophobic part: Ra and Rb constitute a kind of “twin tail” of the surfactant. The compositions of the invention does not need to make use of branched Ra and Rb groups which are more costly than linear Ra and Rb groups.
According to a first embodiment, the group A is a carboxylate group, optionally protonated in all or part (and preferably partially only). In that case the surfactant of the invention is a betaine of the formula (I-1):
wherein Ra, Rb, Rc, Rd, (E1) and (E2) have the meaning given herein-above for formula (I). Typically, in the surfactants of formula (I-1), (E1) is a divalent alkanediyl radical of formula —(CH2)n— wherein n=1, 2, 3 or 4, preferably 2 or 3 (most typically 3) and (E2) is a divalent alkanediyl radical of formula —(CH2)n— wherein n=1, 2 or 3, preferably 1 or 2 (most typically 1);
and wherein:
According to a second possible embodiment, the group A is a sulfonate group —SO3−, optionally protonated in all or part (and preferably partially only). In that case the surfactant of the invention is a betaine of the formula (I-2):
wherein Ra, Rb, Rc, Rd, (E1) and (E2) have the meaning given herein-above for formula (I). Typically, in the surfactants of formula (I-2), (E1) is a divalent alkanediyl radical of formula —(CH2)n— wherein n=1, 2, 3 or 4, preferably 2 or 3 (most typically 3) and (E2) is a divalent alkanediyl radical of formula —(CH2)n— wherein n=2, 3 or 4 that may carry an —OH group, typically a —CH2-CHOH—CH2- group;
and wherein:
The invention also relates to mixtures containing at least two distinct surfactants matching the generic definition of formula (I), for example:
According to another aspect, the invention relates to a method for preparing the surfactant having the formula (I) as defined herein-above.
This method includes the following steps:
The surfactants of the invention may be easily prepared from cheap and available (typically naturally occuring) raw materials of relatively low cost, which is a first avantage.
Their three-step preparation process further more allows a good control of their functionalization, which give an access to well defined tailor made molecular structures. By carefully choosing the chain length of the starting fatty acids, it's possible to control the chain length of the fatty ketone and therefore the structure of the final surfactant which allows fine tuning of the properties of the final product.
In addition, according to a specific embodiment, the hydrophobic part of the surfactants of the invention can be entirely saturated, which provides stability against oxidation when compared to unsaturated products.
According to yet another aspect, a subject-matter of the invention is the use of the surfactants of formula (I) for oil recovery, especially for enhanced oil recovery operations.
The inventors have found in the scope of the work which has led to the instant invention that the surfactants of formula (I) have an interesting structure (with a relatively long hydrophobic chain having a polar moiety attached sensibly in the middle (exactly in the middle when Ra═Rb, the exact position depending of the nature of Ra and Rb). These compounds are of particular interest for EOR application.
More details and preferred embodiments are set forth in the detailed specification hereinafter.
The Zwitterionic Surfactants and their Preparation
The Ra and Rb groups present in the surfactants of formula (I) may be defined by the acids RaCOOH and RbCOOH from which they are prepared in step 1 as defined herein-above (and also referred herewith as “fatty acids”), or from which they could have been prepared in the case they are not prepared by making use of this step.
Preferred fatty acids from which the surfactants of formula (I) are actually derived (or theorically derivable) are caprylic acid, capric acid, lauric acid, myristic acid, palmitic acid, stearic acid, naphthenic acids, isostearic acid, arachidic acid, behenic acid, lignoceric acid, cerotic acid or mixtures thereof and preferred acid derivatives are the esters and anhydrides of these acids. Preferred are caprylic acid, capric acid, lauric acid, myristic acid, palmitic acid, stearic acid, naphthenic acids, isostearic acids or mixture thereof.
Other fatty acids from which the surfactants of formula (I) are actually derived (or theorically derivable) comprise one or more double bonds in the chain and include for example oleic acid, linoleic acid, linolenic acid and erucic acid to name only a few examples.
Yet other fatty acids from which the surfactants of formula (I) are actually derived (or theorically derivable) comprise the so called naphthenic acids. The term “naphthenic acid” herein generally denotes a complex mixture of saturated monocarboxylic acids containing cyclopentyl and/or cyclohexyl fragments containing usually 9 to 20 carbon atoms. Naphthenic acids are obtained by oxidation of the naphtha fraction of crude oil and their composition varies with the crude oil composition and the conditions during refining and oxidation.
Preferably, the surfactants of formula (I) are actually prepared from an internal ketone obtained from fatty acids according to step 1 of the process as defined herein-above. In that case, the surfactants of formula (I) may either be obtained from a single fatty acid RaCOOH or from a starting fatty acids mixture. In the case of a mixture of fatty acids, said mixture may be for example a so-called “cut” as typically obtained from vegetable or animal oils through saponification or alcoholysis. More preferably, it may be a fatty acid cut derived from coconut oil or palm kernel oil, that preferably contains a mixture of fatty acids which can comprise fatty acids having 8 carbon atoms up to 18 carbon atoms.
Internal ketones used in step 2 of the process described herein above can alternatively be obtained through cross-ketonization reactions starting from a mixture of linear fatty acids and naphthenic acids, or through cross-ketonization starting from a mixture of aliphatic fatty acids and benzoic acid.
The surfactants of the invention may advantageously been prepared in the following conditions:
In this reaction step, fatty acids, preferably saturated straight chain fatty acids, are transformed into the internal ketone (II) through a decarboxylating ketonization reaction. This reaction is typically conducted with the fatty acids in a liquid phase and preferably by continuously removing water formed during the reaction from the reaction mixture.
Step 1 can be applied to a single fatty acid or to a cut of fatty acids generating therefore a cut of fatty ketones of formula (II). Typically the prepared fatty ketones of formula (II) contain the carbonyl group sensibly in the middle of the chain (exactly in the middle when a single fatty acid is used: Ra═Rb, the ketone is symetrical—when starting from a cut of fatty acids, all the possible ketones (II) are formed by combination of the different chains of the starting fatty acids, with a distribution of ketones obtained after the reaction following sensibly a statistical binomial law).
Typically, step 1 may be catalyzed by at least one metal compound, advantageously selected from the group consisting of Mg, Ca, Al, Ga, In, Ge, Sn, Pb, As, Sb, Bi, Cd and transition metals having an atomic number of from 21 to 30 or a mixture thereof or an oxide of these metals or a mixture thereof, preferably in an oxydized state (the metal in its oxidized state may be generated in situ by introducing the corresponding metal at a non oxidized state).
The reaction of step 1 is advantageously catalyzed by compounds of oxydized iron, typically at least one iron oxide, such as magnetite Fe3O4, and/or Fe2O3, and/or FeO, the at least one iron oxide being preferably generated in situ in step 1 by introducing metallic iron, typically iron powder (namely: Fe(0)) which has the advantage to be a very cheap and abundant material.
When step 1 is carried out in the presence of a metal compound of the type recited above, especially metallic iron, it is advantageous that step 1 comprises two successive stages, namely:
After stage (1.2), it can be interesting to separate the metallic compounds from the products (that may be done using conventional techniques) and then to recycle the metallic compounds, e.g. for the conversion of another batch of fatty acids
The fatty acids used in the two stages (1.1) and (1.2) preferably comprise at least 10 mol %, based on the entire amount of fatty acids, of fatty acids having 12 carbon atoms or less. Typically, the fatty acids are selected from butanoic acid, hexanoic acid, isostearic acids, caprylic acid, capric acid, lauric acid, myristic acid, palmitic acid, stearic acid, arachidic acid, behenic acid, lignoceric acid, cerotic acid or mixtures thereof, and more preferably the fatty acids comprise 8 to 18 carbon atoms.
Stages 1.1 and 1.2 can also be operated on fatty acid derivatives preferably selected from esters and anhydrides, such as esters or anhydrides of caprylic acid, capric acid, lauric acid, myristic acid, palmitic acid, stearic acid, arachidic acid, behenic acid, lignoceric acid, cerotic acid or mixtures thereof (these derivatives are made preferably from fatty acids containing 8 to 18 carbon atoms).
Step 1 of the process may for example be conducted by:
At the end of stage (b), the products fatty ketone can be separated from iron compounds, for example as follows:
(Preparation of Intermediate III)
This step allows a reductive amination of the ketone (II) obtained in step 1.
This reductive amination is preferably performed by reacting the ketone (II) and the diamine of formula H2N-(E1)-NRcRd as defined herein-above in the presence of a transition metal (e.g. Ni, Co, Cu, Fe, Pd, Pt) based catalyst (typically Pd/C), under hydrogen pressure (typically between 1 atm. and 200 bar).
According to a possible embodiment, the reaction is carried out in a solvent. However, the presence of such a solvent is not compulsory and according to a specific embodiment, no solvent in used in step 2. The exact nature of the solvent, if any, may be determined by the skilled person. Typical suitable solvents include, without limitation, methanol, ethanol, isopropanol and mixtures thereof.
Besides, Step 2 is usually carried out at a temperature ranging from 15° C. to 300° C.
Step 2 may be conducted batchwise, semi-continuously or continuously and generally performed either in a batch mode or in a continuous mode using a fixed-bed catalyst (gas-solid or gas-liquid-solid process).
A diamine of formula H2N-(E1)-NRcRd suitable for step 2 is dimethylaminopropylamine (DMAPA). This amine can be employed in stoichiometric amounts or in excess.
Other example of diamines suitable in step 2 include aminoethylethanolamine (AEEA) and ethylendiamine (FDA).
According to a specific embodiment, the group -(E1)- of the diamine of formula H2N-(E1)-NRcRd may comprise an amine group (in that case, the amine may be a triamine: the term “diamine” as used in step 2 intend to encompass compounds including at least two amine group, and optionally more). Examples of amines with more that two amine groups include for example diethylene triamine (DETA), triethylenetetramine (TETA), tetraethylene pentamine (TEPA)
Mixtures of diamines may also be used, including for example mixture of DETA/EDA/AEEA
The product (III) of step 2 can be recovered after catalyst separation and removal of solvent and DMAPA excess. Finally the product can be purified, e.g. using standard technics such as distillation.
Step 3: Preparation of the Surfactant from Compound (III)
Grafting the group -(E2)-A on the group —NRcRd of the compound of formula (III) obtained in step (2) can be made by the methods described herein or by any technic known by the skilled person.
For preparing the compound (I-1), step 3 generally comprises a reaction of the compound (III) with a compound of formula X-(E2)-COOH (preferably deprotonated in all or part in the form of a carboxylate) wherein (E2) is as defined herein-above for formula (I-1) and X is a leaving group, typically an halogen atom such as Cl (Cl is especially suitable) or Br or I, or a sulfonate (optionally substituted for example an alkyl or arylsufonate), a sulfate or a triflate. The compound X-(E2)-COOH may for example be monochloroacetic acid, used in the form of the acetate, for example added as sodium monochloroacetate.
Alternatively, a grafting of a —COOH group may be obtained by reacting the compound (III) with acrylic acid or derivatives thereof.
The reaction may be carried out in a solvant (iPrOH for example). Typically, the reaction is carried out at 25 to 150° C., for example from 50 to 100° C.
For preparing the compound (1-2), step 3 may for example comprise a reaction of the compound (III) with a compound of formula X-(E2)-SO3H (optionally deprotonated in all or part in the form of sulfonate) wherein (E2) is as defined herein-above for formula (I-2) and X is a leaving group, typically an halogen atom such as Cl (Cl is especially suitable) or Br or I, or a sulfonate (optionally substituted for example an alkyl or arylsufonate), sulfate or triflate. The compound X-(E2)-SO3H may for example be chlorohydroxypropanesulfonic acid, used in the form of the sulfonate, for example added as sodium chlorohydroxypropanesulfonate. A similar conversion of compound (III) into compound (I) is obtained by reacting the compound (III) together with epichlorhydrin (EPI) and then with sodium bisulfite.
The reaction may carried out in a solvant (iPrOH for example). Typically, the reaction is carried out at 25 to 150° C., for example from 50 to 100° C.
The surfactants according to the invention are of specific interest in EOR applications.
For example, they give rise to low interfacial tension with model alkanes (e.g. dodecane), especially in combination with other hydrophilic surfactants that may improve their solubility in brines applications. One subject-matter of the invention is a method for extracting oil from a subterranean formation, preferably an EOR method, wherein a surfactant of formula (I) is injected in the subterranean formation, preferably in admixture with other hydrophilic surfactants. The invention also relates to the EOR formulations useful in this connection, that comprise at least one surfactant of formula (I), preferably in admixture with other hydrophilic surfactants.
Besides, the surfactants of formula (I) can be used in foam formulations and more particularly low interfacial tension foam formulations once they are mixed with a more hydrophilic anionic surfactant.
One subject-matter of the invention is a method for extracting oil from a subterranean formation, wherein a foam is formed within the subterranean formation, including at least a surfactant of formula (I), preferably mixed with a more additional hydrophilic surfactant.
By way of example of additional surfactants useful with the surfactants of formula (I), one may mention nonionic surfactants, such as alkoxylated nonyl phenol, alkoxylated dinonylphenol, and alkoxylates of various straight and branched alcohols having a carbon chain of preferably from 8 to about 20 or more carbon atoms may be mentioned here. These additional surface active components may also be carboxylated, phosphated, sulfated or sulfonated, i.e. ionized upon use.
The surfactant of the invention may also be use in admixture with other zwitterionic surfactants, (sulfo)betaine surfactants.
A preferred group of additional hydrophilic surfactants which may be used together with the surfactants of formula (I) are alkyl glyceryl ether sulfonates (AGES).
Alkyl glyceryl ether sulfonates (AGES) are well known as detergents utilized in personal care cleansing products and are commercially available from a number of sources. The skilled person will select the best suited AGES based on his professional experience and adapted to the specific case of use so that no further details needs to be given here.
Processes for the manufacture of AGES are described in U.S. Pat. Nos. 3,024,273 and 2,989,547 to which reference is made herewith for further details.
Other surfactants useful in combination with the surfactants of formula (I) are alkoxylated alkyl glyceryl ether sultanates (AAGES) which differ from the alkyl glyceryl ether sulfonates described above by the presence of one or more alkoxy groups between the last carbon atom of the article group and the oxygen atom of the alkyl glyceryl ether sulfonate. AAGES may be represented by the following general formula:
R—O—[—CH2—CH(CH3)—O]n—[—CH2—CH2—O]p—CH2CH(OH)—CH2—SO3−
wherein R is a alkyl chain, and n and p are integers of from 0 to 30, preferably of from 2 to 15 and n and p cannot be both equal to 0.
The compositions in accordance with the present invention can contain additional ingredients which are customary ingredients of surfactant flooding compositions for enhanced oil recovery processes.
The way of use of the compositions of the present invention in enhanced oil recovery processing is known to the skilled person and has been described in the literature so that no further details need to be given here. The skilled person will decide on the best process based on his professional experience and taking into account the specific circumstances of the individual application case.
The appended examples illustrate in details preparation of surfactants of the invention and their interest in EOR applications.
The reaction was carried out under argon in a round bottom flask equipped with mechanical stirring, dean stark apparatus and an addition funnel.
In the reactor, 700 mg of iron powder were dispensed and 20 g of lauric acid was then introduced in the addition funnel. The reaction was conducted as follows:
At the end of the reaction, the addition funnel was replaced by a distillation apparatus and the products were distilled off at 290° C.−340° C. under 50 mbars pressure.
Then the distillation apparatus was again replaced by the addition funnel containing a new amount of 5 g+15 g of fatty acids and the operations described above were repeated for another cycle.
Importantly, no additional amount of iron was introduced. This possible recycling of iron is a generic advantage of step 1: the residue in the flask remaining after distillation is efficient to convert the next batch of acids.
Overall 4 cycles have been carried out without any loss of performances reducing therefore the concentration of iron to less than 1 wt % relative to total fatty acids amount converted.
A cut of saturated straight chain fatty acids with a distribution representative of natural coconut oil (C8: 7 wt %, C10: 8 wt %, C12: 48 wt %, C14: 17 wt %, C18: 10 wt % and C18: 10 wt %) was used in this case.
The reaction was carried out under argon in a round bottom flask equipped with mechanical stirring, dean stark apparatus and an addition funnel.
In the reactor, 3.3 g of iron powder were dispensed and a total 100 g of melted fatty acids were introduced in the addition funnel. The reaction was conducted as follows:
After complete conversion of fatty acids and the intermediate complex, the mixture was then allowed to cool down at room temperature and 200 mL of CHCl3 was added into the reaction vessel.
The suspension was filtered on a silica plug (600 g) and the remaining product was eluted with additional volume of CHCl3. After evaporation of the solvent, 140 g of the sought product (82% isolated yield) was recovered as a white wax.
In a 500 mL round bottom flask equipped with magnetic stirring and condenser are added 10 g (29.56 mmol) of the tricosanone as prepared in example 1.1.1., 120 mL of THE and finally 9.3 mL of DMAPA (73.8 mmol).
The mixture was stirred at room temperature during 1 hour in order to solubilize the ketone and 17.5 mL of Ti(OiPr)4 (59.12 mmol) is added to the reaction mixture which is then stirred at room temperature during 12 hours.
50 mL of MeOH were then added to the mixture followed by the careful addition of 1.7 g of NaBH4 (44.34 mmol). The resulting mixture was then stirred during 4 h00 and 250 mL of Et2O followed by 250 mL of H2O are added into the reaction vessel. Upon addition of water a white precipate of TiO2 was formed which and then removed by filtration.
The organic phase of the filtrate is separated from the aqueous phase and is washed twice with 500 mL of aq. NaOH solution (0.5 M) followed by 500 mL of brine. The organic phase is dried over MgSO4, filtered and evaporated to give a pale yellow oil.
The product is finally purified by flash chromatography on silica gel using CH2Cl2: MeOH as eluent (from 70:30 to 60:40) to obtain 6 g of the product as a transparent oil. (48% yield).
The same protocol was applied with the product as prepared in example 1.2.1 starting from the compound as prepared in example 1.1.2
In a 50 mL round bottom flask equipped with magnetic stirring and a condenser were successively added 5.57 g of compound prepared in example 1.2.1 (13.12 mmol), 5.5 mL of iPrOH and 6.52 mL of H2O.
1.83 g of sodium monochloroacetate (15.74 mmol) was finally added to the mixture which is stirred at 85° C. during 7 h00. During this time the mixture changes from biphasic to monophasic.
The final betaine solution (35 wt % of active betaine in iPrOH:H2O 40:60) can be used as such.
NMR analysis of the mixture shows complete conversion of starting diamine and confirms that quaternization takes place exclusively and the tertiary amine moiety of the starting diamine.
Same protocol as in 1.3.1 was employed for the synthesis of mixture of betaines from compound prepared in example 1.2.2 The product was obtained in a H2O:iPrOH (60:40) solution (35 wt % active betaine)
In a 50 mL round bottom flask equipped with a mechanical stirring and a condenser 4.18 g of compound prepared in example 1.2.1 (9.84 mmol), 3.4 mL of iPrOH and 4.1 mL of H2O are added. The mixture is allowed to stir at room temperature and addition of 2.32 g of sodium chlorohydroxypropanesulfonate (11.8 mmol).
The mixture is then stirred at 85° C. during 8 h00. During the course of the reaction, the media changes from biphasic to monophasic.
NMR analysis of the crude shows complete conversion of starting diamine and clean formation of sultaine.
The product is obtained in a H2O:iPrOH (60:40) solution (42 wt % active betaine) and is used as such.
Same protocol as in 1.3.3 was employed for the synthesis of mixture of the compound prepared in example 1.2.2.
Starting from log of ketones, 6 g of pure diamines are obtained after purification (48% yield).
The surfactants prepared in example 1 (compounds prepared in examples 1.3.1; 1.3.2; 1.3.3; 1.3.4) were mixed with various hydrophilic zwitterionic surfactants.
In contrast to anionic surfactants, betaines of the invention are less sensitive to physicochemical environment changes, i.e. salinity, temperature. Changing the weight ratio between the two zwitterionic surfactants was actually the best way to optimize the formulation and obtain the appropriate phase behavior.
2.1 In the following examples, the performances of surfactants formulations containing the betaine of example 1.3.1 in a brine solution at 50 g/L NaCl were compared.
The total surfactant concentration was set at 8 g/L and the formulation variable was the wt. % of the more hydrophilic zwitterionic surfactant (considered as co-surfactant) in the surfactant blend.
The wt. % of the more hydrophilic zwitterionic leading to a Will phase behavior (optimal wt %. of co-surfactant), was determined in presence of crude oil at 40° C. and reported in Table 1. The solubility of surfactant blends was also analyzed.
obtained from 2-butyloctanoic acid (typically C12- Guerbet acid e.g. ″Isocarb12″ from Sasol) through condensation with DMAPA (3-dimethylaminopropyl amine) followed by a reaction with sodium monochloroacetate.
2.2. In terms of interfacial tension, all the blends studied led to ultra-low values (<10−2 mN/m). On the other hand, only the hydrophilic amido betaine derived from a branched C12 acid (ADBB12) allows obtaining a homogeneous but opalescent water solution (absorbance of 0.46) at the optimal formulation (71 wt. %).
All the linear alkyl betaines, solutions separate in two phases or forms really turbid solutions (0.86 absorbance). Interfacial tension with crude oil of the mixture ADBB12 and the betaine from C23 ketones derived diamine at the optimal wt. % was evaluated by spinning drop methods. The ultra-low interfacial tension was confirmed (=10−3 mN/m).
The betaines derived from C15-C35 ketones mixture have similar behavior than the C23 ketones.
Evaluation of the Sultaine Derived from C23 Diamine
Sulfobetaine was tested at the same conditions as the betaines obtained from C23 ketone derived diamine. Results are presented in table 2.
As the sulfobetaine from C23 ketone derived diamine is more hydrophilic than the betaines form, lower concentration in co-surfactant (ADBB 12) is needed to achieve Will phase behavior. Furthermore, increasing the concentration of sulfobetaine displace the middle phase microemulsion to a less soluble water region. Same effect is expected using the co-surfactants mentioned in table 1.
Hence betaines from long alkyl chain ketones derived diamine can be used to obtain optimal performances (solubility and interfacial tension) once blended with a more hydrophilic zwitterionic surfactant. Such mixtures can be robust to handle salinity changes in reservoir conditions.
| Number | Date | Country | Kind |
|---|---|---|---|
| 16305409.1 | Apr 2016 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2017/057493 | 3/30/2017 | WO | 00 |
