Patent Publication Number: US-4733727-A

Title: Oil recovery with water containing carbonate salt, CO2, and surfactant

Description:
RELEVANT APPLICATION 
     The Assignee&#39;s co-pending application Ser. No. 928,123, &#34;Oil Recovery with Water Containing Carbonate Salt and CO 2 ,&#34; which lists as the inventors A. H. Falls and M. I. Kuhlman, is relevant to this application. 
     BACKGROUND OF THE INVENTION 
     This invention relates to a fluid drive oil recovery process in which CO 2 , water and surfactant are injected into an oil reservoir to displace the oil. More particularly, the invention relates to a method for reducing the extent to which surfactant is lost due to its adsorption on the reservoir rocks. 
     In some respects, the present invention is an improvement on the process described in U.S. Pat. No. 4,502,538 by S. L. Wellington, J. Reisberg, E. F. Lutz and D. B. Bright. In that process, oil is displaced within a subterranean reservoir by injecting a combination of substantially liquefied CO 2 , brine and a polyalkoxy aliphatic surfactant material. The disclosures of that patent are incorporated herein by reference. 
     The present invention also improves processes of the type described in U.S. Pat. No. 3,529,668. The latter relates to an oil recovery process in which a bank of foam is established by an injection of a foaming surfactant, an aqueous liquid and a gas such as CO 2 . 
     SUMMARY OF THE INVENTION 
     The present invention relates to an improvement in an oil recovery process in which CO 2 , aqueous solution and an anionic surfactant are injected into a subterranean reservoir to displace oil, with the injection pressure and rate of fluid production arranged so that the CO 2  is pressurized to at least more than the reservoir fluid pressure. The improvement relates to reducing the extent to which the surfactant is absorbed on the reservoir rocks. This is effected by including within the aqueous phase of the injected fluid an amount of monovalent cationic salt of carbonic acid effective for increasing the pH of the solution, at the conditions encountered within the reservoir, to an extent which reduces the level of adsorption of the surfactant. 
     In the present process the CO 2  is preferably pressurized to a point of significant interaction with the oil, such as the point where either (1) it becomes substantially miscible with the reservoir oil or (2) enough mass transfer occurs between the injected CO 2  and the reservoir oil that (a) the viscosity of the reservoir oil is lowered and/or (b) the reservoir oil swells and/or (c) the CO 2  is able to extract components from the reservoir oil. 
    
    
     BRIEF DESCRIPTION OF THE DRAWING 
     FIG. 1 shows a plot of aqueous liquid solution pH with increasing amounts of sodium bicarbonate or sodium carbonate at 170° F. and 2500 psig. 
     FIG. 2 shows a similar plot at 77° F. and 14.7 psia. 
    
    
     DESCRIPTION OF THE INVENTION 
     Dilute aqueous solutions of anionic sulfonate surfactant, such as Enordet® alcohol ethoxy glycerol sulfonates (AEGS), supplied by Shell Chemical Company, NEGS, ethoxyglyceryl sulfonates synthesized by Shell Development Company from NEODOL® alcohol ethoxylates supplied by Shell Chemical Company, and other alcohol ethoxylates, and NES alcohol ethoxy sulfonates, available from Diamond Shamrock Company, may be capable of preventing CO 2  from overriding other phases during a CO 2  oil recovery process in nearly horizontal Gulf Coast sandstones. Because the mobility of CO 2  in the absence of surfactant is high, it is desirable that the surfactant front remain ahead of the CO 2  front. 
     One way of keeping the surfactant front ahead of the CO 2  front is to inject a large preslug of surfactant solution followed by alternate slugs of CO 2  and surfactant solution. This approach has the advantage that the surfactant in the preslug is transported through the reservoir at neutral pH. When CO 2  is introduced, however, the pH drops due to the increase in the concentration of carbonic acid in the solution. The pH reduction causes the surfactant concentration to be diminished as the pH approaches or falls below the point of zero charge of the reservoir rock materials, such as silica and clay, and increases the adsorption onto the rocks. Thus, the preslug design succeeds only if the concentration of surfactant in the brine behind the CO 2  front is sufficient to control CO 2  mobility. 
     The preslug design also has other drawbacks. The size of the slug needed to ensure that surfactant stays ahead of CO 2  throughout the reservoir is large. As such, the economics of the process suffer because several years elapse before the oil displacing agent (CO 2 ) is even introduced. Moreover, there is the risk that CO 2  may not invade the same volume as the surfactant solution before it. 
     A much more attractive way of keeping the surfactant front ahead of the CO 2  front is to alternately inject surfactant solution and CO 2  from the start. In this way, oil can be produced earlier in the life of the project. In prior processes, this caused the surfactant to be transported at relatively low pH. However, the adsorption losses for CO 2  -foam-forming NEGS, NES or Enordet® 2000 series surfactants at low pH (e.g. on the order of 3) are larger than at neutral pH. For example, the adsorption of 0.05 wt% NEGS 9-2.6 sulfonate based on C 9  alcohol from 70% D-sand water of pH 6.8 at 170° F. onto a relatively clean, Ottawa sand is about 0.069 lb m  surfactant per barrel of pore space and onto Ottawa sand containing 2 wt% Silver Hill illite is about 0.13 lb m  surfactant per barrel of pore space. In the presence of CO 2  at 170° F., 2600 psig, these adsorptions rise to 0.098 and 0.22 lb m  surfactant per barrel of pore space, respectively. 
     The reactions that take place in an aqueous solution in equilibrium with CO 2  are complex. When a carbonate solution contains divalent cations, solid phases may form. Whether solids precipitate can be determined by comparing the solubility products of the various minerals with the products of the aqueous phase concentrations of the appropriate ions; the least soluble of these is calcium carbonate. When equations for the equilibrium constants for reactions between the various ionic species are combined with a charge balance and stoichiometric relationships, they yield a cubic equation for the concentration of hydrogen ions in solution. For example, ##EQU1## when the carbonate salt is Na 2  CO 3 , NaHCO 3 , or a mixture of Na 2  CO 3  and NaHCO 3 . The solution to such an equation can be found, either analytically or by simply evaluating the polynomial as a function of [H +  ] to determine the pH at which it changes sign. The ions from the salts in the brine do not appear in this equation because their contributions cancel one another. The brine does play a role, however, as it affects the activities of the solutes and the apparent concentration of carbonic acid. 
     The values of the equilibrium constants and apparent concentration of carbonic acid used in finding solutions to the above equation are recorded in Table 1. The brine was modeled as 30% synthetic D-sand water (DSW) because it has nearly the same salinity as seawater (see Table 2), for which the appropriate equilibrium constants have been measured and correlated. These correlations are applied directly to 30% DSW to produce the values shown in Table 1. Although 30% DSW has less total dissolved solids than water available for CO 2  field projects in Gulf Coast sands, the calculation presented here should qualitatively reflect aqueous carbonate equilibria in more concentrated brines. 
     
                       TABLE 1                                                     
______________________________________                                    
Consistent with Molal Units, Values of the Equilibrium                    
Constants and Apparent Concentration of Carbonic Acid used                
to Determine the pH of Carbonated, 30% D-sand Water                       
to which Na.sub.2 CO.sub.3 or NaHCO.sub.3 is added                        
                 Value @  Value @                                         
                 170° F.                                           
                          77° F.                                   
Quantity         2500 psig                                                
                          14.7 psig                                       
______________________________________                                    
-log K.sub.w     11.9     13.2                                            
-log K.sub.1     6.0      5.95                                            
-log K.sub.2     8.51     9.04                                            
-log K.sub.sp.sup.CaCO.sub.3                                              
                 6.57     6.19                                            
[H.sub.2 CO.sub.3 (app)]                                                  
                 0.865    0.012                                           
______________________________________                                    
 
    
     
                       TABLE 2                                                     
______________________________________                                    
Comparison of Concentrations of Major Inorganic Species                   
in Seawater and in 30% Synthetic D-sand Water                             
         Concentration in                                                 
                        Concentration in                                  
         30% Synthetic DSW                                                
                        Seawater                                          
Species  (ppm)          (ppm)                                             
______________________________________                                    
Cl.sup.- 21,900         19,000                                            
Na.sup.+ 12,900         10,600                                            
Ca.sup.2+                                                                 
           500            400                                             
Mg.sup.2+                                                                 
           390           1,300                                            
______________________________________                                    
 
    
     FIG. 1 displays the pH of a solution of 30% D-sand water in equilibrium with a free CO 2  phase (or CO 2  -rich phase) at 170° F., 2500 psig as a function of Na 2  CO 3  or NaHCO 3  content. This is representative of such a solution under reservoir conditions as a function of the amount of Na 2  CO 3  or NaHCO 3  added. The pH rises quickly when Na 2  CO 3  is included. This is because Na +  is being substituted for H +  in satisfying the charge balance. Whether Na 2  CO 3  or NaHCO 3  is incorporated, however, makes little difference on the pH of the system: it is the equivalents of Na +  that counts. Thus, the ratio of NaHCO 3  to Na 2  CO 3  needed to achieve a given pH is equal to twice the ratio of the molecular weights. 
     There is one difference between Na 2  CO 3  and NaHCO 3 . The solution takes up CO 2  to maintain equilibrium with the free CO 2  phase when Na 2  CO 3  is added. By contrast, CO 2  evolves from the solution when NaHCO 3  is used. In either case, the amount of CO 2  is small, corresponding to less than 5 SCF/bbl of solution for the concentration range depicted in FIG. 1. 
     For this example, the solubility product of CaCO 3  is exceeded when the concentrations of Na 2  CO 3  and NaHCO 3  reach approximately 0.42 wt% and 0.67 wt%, respectively. To keep CaCO 3  from precipitating, the concentrations of the additives must be below these values. The amounts that can be added decrease as the hardness increases. 
     The equilibrium state differs greatly at surface conditions, e.g., 77° F. and low pressure. In particular, calcium carbonate precipitates from the solution at lower levels of Na 2  CO 3  or NaHCO 3 . 
     If a free CO 2  phase is not present, as would ordinarily be the case in surface facilities, CaCO 3  drops out of the 30% DSW solution, at a pH slightly below 9, when only 0.0012 wt% Na 2  CO 3  has been added. The case of adding NaHCO 3  is somewhat better: 0.0168 wt% can be incorporated before CaCO 3  precipitates (solution pH of 7.5). Nevertheless, neither of these chemicals can be added in quantities sufficient to raise the solution pH appreciably under reservoir conditions, as indicated in FIG. 1. 
     A way to keep calcium carbonate from precipitating in surface facilities is to store the solution under a blanket of CO 2 . The partial pressure of the CO 2  can be relatively low. FIG. 2 displays the calculation of solution pH as a function of the Na 2  CO 3  or NaHCO 3  content when the partial pressure of CO 2  is one atmosphere. 0.15 wt% Na 2  CO 3  or 0.24 wt% NaHCO 3  can be added to the brine before CaCO 3  drops out. (Even more Na 2  CO 3  or NaHCO 3  can be included if the partial pressure of CO 2  is higher.) These amounts give a pH of about 4.5 under reservoir conditions (see FIG. 1). 
     Because the surfaces of reservoir sands become less negatively charged as pH is lowered, raising the pH of a foam formulation from 3 to 4.5 should substantially reduce the adsorption of anionic, CO 2  -foam-forming surfactants. In fact, this has been found experimentally to be the case. With only 0.15 wt% Na 2  CO 3  included in the aqueous solution, the adsorption of 0.05 wt% NEGS 9-2.6 NRE in 70% D-sand water in equilibrium with CO 2  at 170° F. and 2600 psi was found to be 0.073 lb m  surfactant per barrel of pore space on relatively clean Ottawa sand and 0.17 lb m  surfactant per barrel of pore space on Ottawa sand containing 2 wt% Silver Hill illite. 
     In a preferred procedure for conducting the present invention, fluid is circulated between injection and production locations within the reservoir at a rate providing both a relatively high pressure at which the CO 2  is pressurized to a point of significant interaction with the reservoir oil and a suitable rate of flow, with the mobility of the injected fluid at least substantially equalling that of the water or brine in the reservoir. Then, while maintaining substantially the same rate of circulation, portions of CO 2 , at least one relatively water-soluble anionic surfactant and portions of an aqueous solution containing an effective amount of an alkali metal salt of carbonic acid and aqueous liquid having physical and chemical properties at least substantially equivalent to those of the aqueous liquid in the reservoir, are included within the inflowing fluid. The included amount of alkali metal salt is an amount effective for increasing the pH of the solution in contact with the pressurized CO 2  at the conditions within the reservoir to an extent reducing the level of adsorption of the surfactant on the reservoir rocks. That injection is continued until the volume of injected fluid is sufficient to form a bank large enough to be capable of remaining substantially intact throughout a displacement from the injection to the production location within the reservoir. Then, a circulation of fluid comprising said injected fluid or a drive fluid effective for displacing said injected fluid, between the injection and production locations, is continued to displace oil into the production location. 
     The surfactant used in the present process can consist essentially of at least one water-soluble anionic surfactant, such as a polyalkoxy sulfonate surfactant which surfactant is capable of reducing the mobility of the CO 2  and aqueous solution in contact with the reservoir oil (or a substantially equivalent oil). The surfactant preferably has the formula 
     
         RO(R&#39;O).sub.x R&#34;SO.sub.3 M 
    
     where: R is an aliphatic or aliphatic-aromatic hydrocarbon radical containing from about 6 to 25 carbon atoms connected to an oxygen atom. R&#39; is an ethylene radical or a predominantly ethylenic mixture of ethylene and propylene radicals that are each connected between oxygen atoms, x is a number at least equalling 1; R&#34; is a saturated aliphatic C 2  or C 3  hydrocarbon radical or CH 2  CHOHCH 2  radical connected between an oxygen and a sulfur atom; and M is an alkali metal or ammonium ion. 
     The saline aqueous solution (or water or brine) which is used in the present process can be substantially any which can be flowed through the reservoir to be treated without significant change due to dilution and/or increases in salinity due to diffusion and/or ion-exchange effects within the reservoir. Such a brine is preferably the brine produced from the reservoir to be treated or produced from a nearby reservoir. When the reservoir has been waterflooded with a brine less saline than the reservoir brine, the brine used in the present process preferably has a salinity which is substantially equivalent in the effective ratio of monovalent to multivalent cations relative to the brine used in the waterflood after it reached a state of equilibrium with the rocks in the reservoir. 
     A drive fluid used for displacing a bank or slug of fluid containing the dispersion of CO 2  in aqueous surfactant solution (as injected or formed within the reservoir by the injected substantially liquefied CO 2 , brine and surfactant) through a reservoir can be substantially any drive fluid which is capable of displacing such a mixture within a reservoir formation. Particularly suitable fluids comprise aqueous liquids and/or mixtures of aqueous liquids and gas having mobilities at least substantially as low as that of said bank of fluid. Suitable fluids can comprise water, brine, carbonated water, flue gas, nitrogen, etc. 
     The monovalent cationic salt of carbonic acid which is used in the present process can comprise substantially any alkali metal or ammonium salt. Sodium carbonate, sodium bicarbonate, or mixtures of them, are particularly preferred for such use.