Patent Publication Number: US-10316260-B2

Title: Carbon dioxide fractionalization process

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
     This application is a continuation of U.S. patent application Ser. No. 14/200,346, filed Mar. 7, 2014, which is a divisional of U.S. patent application Ser. No. 12/824,382, filed Jun. 28, 2010, now U.S. Pat. No. 8,709,215, which is a divisional of U.S. patent application Ser. No. 11/621,913 filed Jan. 10, 2007, now Reissued U.S. Pat. No. RE 44,462, the contents of all of which are incorporated herein by reference as if reproduced in their entireties. 
    
    
     STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH OR DEVELOPMENT 
     Not applicable. 
     REFERENCE TO A MICROFICHE APPENDIX 
     Not applicable. 
     BACKGROUND 
     Carbon dioxide is a naturally occurring substance in most hydrocarbon formations. While the carbon dioxide concentration will depend on the location of the formation, carbon dioxide concentrations as high as eighty percent are common in many areas, such as West Texas. Moreover, the implementation of tertiary recovery operations, such as carbon dioxide injection into the subterranean wellbore, can increase the carbon dioxide concentration within the produced hydrocarbons. In either case, the carbon dioxide concentration of the produced hydrocarbons may be sufficiently high to require the carbon dioxide concentration to be reduced before the hydrocarbons can be refined or further processed. 
     Several solutions are known for reducing the carbon dioxide concentration or “sweetening” a hydrocarbon stream. For example, amine processes, physical solvent processes, membrane processes, and carbon dioxide recovery processes have all been used to sweeten hydrocarbon streams. The processing facilities employing these hydrocarbon sweetening processes are generally sized for a specific processing capacity and hydrocarbon feed stream composition. As such, when the carbon dioxide concentration of the hydrocarbon feed stream increases or additional feedstock comes online, then an additional processing facility must be constructed to compensate for the change in hydrocarbon feed stream composition or the increased feedstock. The construction of a new processing facility is undesirable because of the substantial capital cost, operating costs, and time delay inherent in such a solution. 
     SUMMARY 
     In one aspect, the disclosure includes a method comprising separating a hydrocarbon feed stream having carbon dioxide into a heavy hydrocarbon stream and a light hydrocarbon stream. The light hydrocarbon stream is separated into a carbon dioxide-rich stream and a carbon dioxide-lean stream. At least a portion of the carbon dioxide-lean stream is fed to a hydrocarbon sweetening process. 
     In another aspect, the disclosure includes a method comprising receiving a hydrocarbon feed stream that comprises 30 molar percent to 80 molar percent carbon dioxide. A heavy hydrocarbon stream is separated from the hydrocarbon feed stream, wherein the heavy hydrocarbon stream comprises at least 90 molar percent C 3+  hydrocarbons. A carbon dioxide-rich stream is separated from the hydrocarbon feed stream, wherein the carbon dioxide-rich stream comprises at least 95 molar percent carbon dioxide. 
     In a third aspect, the disclosure includes a method comprising receiving a hydrocarbon feed stream that comprises carbon dioxide. The hydrocarbon feed stream is separated into a carbon dioxide-lean stream and a carbon dioxide-rich stream. The carbon dioxide-lean stream comprises at least 20 molar percent less carbon dioxide than the hydrocarbon feed stream, and the carbon dioxide-rich stream comprises less than 10 molar percent hydrocarbons. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         FIG. 1  is a process flow diagram of one embodiment of the carbon dioxide fractionalization process; and 
         FIG. 2  is a process flow diagram of another embodiment of the carbon dioxide fractionalization process. 
     
    
    
     DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS 
     Disclosed herein is a carbon dioxide fractionalization process that may be positioned in front of an existing hydrocarbon sweetening process to increase the processing capacity of the hydrocarbon sweetening process. Specifically, the carbon dioxide fractionalization process purifies the hydrocarbon feed stream by removing at least some of the carbon dioxide and the heavy hydrocarbons from a hydrocarbon feed stream. The purification of the hydrocarbon stream reduces the carbon dioxide and heavy hydrocarbon loading on the hydrocarbon sweetening process, thereby increasing the processing capacity of the hydrocarbon sweetening process. Furthermore, the carbon dioxide fractionalization process produces a carbon dioxide-rich stream that may be injected into a subterranean formation. 
       FIG. 1  illustrates one embodiment of the carbon dioxide fractionalization process  100 . The carbon dioxide fractionalization process  100  separates a hydrocarbon feed stream  200  into a heavy hydrocarbon stream  254 , an acid gas stream  250 , a carbon dioxide-rich stream  244 , and a carbon dioxide-lean stream  234 , the compositions of which are discussed in detail below. The carbon dioxide fractionalization process  100  receives the hydrocarbon feed stream  200  and may pass the hydrocarbon feed stream  200  through a heat exchanger  102  that uses the cooled carbon dioxide-lean stream  232  to reduce the temperature of the hydrocarbon feed stream  200 . A first separation unit  101  that comprises one or more of a separator  108 , a reboiler  110 , a condenser  132 , and a separator  134  may then remove the heavy hydrocarbons from the cooled hydrocarbon feed stream  202 . Specifically, the separator  108  separates the cooled hydrocarbon feed stream  202  into a bottom effluent stream  208  and a top effluent stream  214 . The top effluent stream  214  may then be fed into a condenser  132 , which may give off energy  312  by being cooled, and separates the top effluent stream  214  into a reflux stream  246  and a light hydrocarbon stream  248 . Similarly, the bottom effluent stream  208  may be fed into the reboiler  110 , which may receive energy  302  by being heated, and separates the bottom effluent stream  208  into a recycle stream  210  and a heavy hydrocarbon stream  212 . The heavy hydrocarbon stream  212  may then be fed into a separator  134  that separates an acid gas stream  250  from the heavy hydrocarbon stream  252 . The heavy hydrocarbon stream  252  may optionally be cooled by a heat exchanger  114 , for example an air cooler, to produce the heavy hydrocarbon stream  254 . 
     Returning to the light hydrocarbon stream  248 , the light hydrocarbon stream  248  may be fed into a compressor  112  that receives mechanical or electrical energy  304  and increases the pressure and/or temperature of the light hydrocarbon stream  248 , thereby creating a compressed light hydrocarbon stream  216 . The compressed light hydrocarbon stream  216  may then be fed into a heat exchanger  118  that uses a chilled carbon dioxide-lean stream  230  to reduce the temperature of the compressed light hydrocarbon stream  216 , thereby producing a chilled light hydrocarbon stream  224 . A second separation unit  103  that comprises one or more of a separator  120 , a reboiler  124 , and a condenser  122  may then remove at least some of the carbon dioxide from the chilled light hydrocarbon stream  224 . Specifically, the separator  120  separates the chilled light hydrocarbon stream  224  into a heavy effluent stream  236  and a light effluent stream  226 . The light effluent stream  226  may be fed into the condenser  122 , which may give off energy  306  by being cooled, and separates the light effluent stream  226  into a reflux stream  228  and the chilled carbon dioxide-lean stream  230 . The chilled carbon dioxide-lean stream  230  may then be passed through the heat exchangers  118 ,  102  and into a hydrocarbon sweetening process  130 . The hydrocarbon sweetening process  130  may be any process that removes carbon dioxide from a hydrocarbon stream to make the hydrocarbon stream suitable for transportation and/or further processing. Persons of ordinary skill in the art are aware of numerous different hydrocarbon sweetening processes  130 , as illustrated by  Field Processing of Petroleum, Vol.  1 : Natural Gas  by Manning et al., incorporated herein by reference as if reproduced in its entirety. Several examples of the hydrocarbon sweetening process  130  are discussed in detail below. 
     Returning to the separator  120 , the heavy effluent stream  236  may be fed into the reboiler  124 , which may receive energy  308  in the form of heat, and separates the heavy effluent stream  236  into a recycle stream  238  and a cooled carbon dioxide-rich stream  240 . The cooled carbon dioxide-rich stream  240  may optionally be combined with the acid gas stream  250 , if desired. The cooled carbon dioxide-rich stream  240  may then be fed through a heat exchanger  126  that further cools the cooled carbon dioxide-rich stream  240  by removing energy  310  from the cooled carbon dioxide-rich stream  240 , thereby producing the chilled carbon dioxide-rich stream  242 . The chilled carbon dioxide-rich stream  242  may also be fed to a pump  128  that uses energy  314  to pump the carbon dioxide-rich stream  244  to another location, perhaps for injection into a subterranean formation. 
       FIG. 2  illustrates another embodiment of the carbon dioxide fractionalization process  100 . Similar to the embodiment shown in  FIG. 1 , the carbon dioxide fractionalization process  100  shown in  FIG. 2  separates the hydrocarbon feed stream  200  into the heavy hydrocarbon stream  212 , the carbon dioxide-rich stream  244 , and the carbon dioxide-lean stream  234 , the compositions of which are discussed in detail below. The carbon dioxide fractionalization process  100  receives the hydrocarbon feed stream  200  and passes the hydrocarbon feed stream  200  through a heat exchanger  102  that uses the cooled carbon dioxide-lean stream  232  to reduce the temperature of the hydrocarbon feed stream  200 . After the cooled hydrocarbon feed stream  202  exits the heat exchanger  102 , the hydrocarbon feed stream  200  is fed into the optional heat exchanger  104 , which further cools the cooled hydrocarbon feed stream  202  by removing some of its energy  300 , thereby producing a cooled hydrocarbon feed stream  202 . 
     A first separation unit  101  that comprises one or more of separators  106 ,  108  and the reboiler  110  may then remove the heavy hydrocarbons from the cooled hydrocarbon feed stream  202 . Specifically, the cooled hydrocarbon feed stream  202  may be fed into a separator  106  that separates the cooled hydrocarbon feed stream  202  into a light fraction  220  and a heavy fraction  206 . In an embodiment, the light fraction  220  may be a vapor phase and the heavy fraction  206  may be a liquid phase. The light fraction  220  may be combined with the compressed light hydrocarbon stream  216  in a mixer  116  and the heavy fraction  206  may be fed into the separator  108 . The separator  108  separates the heavy fraction  206  into a bottom effluent stream  208  and a top effluent stream  214 . The bottom effluent stream  208  may be fed into a reboiler  110 , which may receive energy  302  by being heated, and separates the bottom effluent stream  208  into a recycle stream  210  and the heavy hydrocarbon stream  212 . The top effluent  214  may be fed into the compressor  112  that receives mechanical or electrical energy  304  and increases the pressure and/or temperature of the top effluent  214 , thereby creating a compressed light hydrocarbon stream  216 . The compressed light hydrocarbon stream  216  may optionally be cooled, for example, by the heat exchanger  114 , which may be an air cooler, to produce a cooled light hydrocarbon stream  218 . The cooled light hydrocarbon stream  218  may then be mixed with the light fraction  220  in the mixer  116 . The resulting mixed light hydrocarbon stream  222  may then be processed as described above for the compressed light hydrocarbon stream  216  in  FIG. 1  to produce the carbon dioxide-lean stream  234 . 
     The hydrocarbon feed stream  200  may contain a mixture of hydrocarbons and carbon dioxide. Numerous types of hydrocarbons may be present in the hydrocarbon feed stream  200 , including methane, ethane, propane, i-butane, n-butane, i-pentane, n-pentane, hexane, octane, and other hydrocarbon compounds. For example, the hydrocarbon feed stream  200  may contain from about 10 percent to about 60 percent methane, no more than about 10 percent ethane, and no more than about 5 percent propane and heavier hydrocarbons (C 3+ ). Although the hydrocarbon feed stream  200  may contain any carbon dioxide concentration, in various embodiments the hydrocarbon feed stream  200  contains from about 10 percent to about 90 percent, from about 30 percent to about 80 percent, or from about 50 percent to about 70 percent of the carbon dioxide. The hydrocarbon feed stream  200  may also include other compounds such as water, nitrogen, hydrogen sulfide (H 2 S), and/or other acid gases. Finally, the hydrocarbon feed stream  200  may be in any state including a liquid state, a vapor state, or a combination of liquid and vapor states. Finally, unless otherwise stated, the percentages herein are provided on a mole basis. 
     Similar to the hydrocarbon feed stream  200 , the carbon dioxide-lean stream  234  may contain a mixture of hydrocarbons and carbon dioxide. Specifically, the composition of the carbon dioxide-lean stream  234  may contain an increased methane concentration and a decreased carbon dioxide concentration compared to the hydrocarbon feed stream  200 . In embodiments, the carbon dioxide-lean stream  234  contains less than about 60 percent, from about 20 percent to about 50 percent, or from about 30 percent to about 40 percent of the carbon dioxide. In yet other embodiments, the carbon dioxide concentration in the carbon dioxide-lean stream  234  is at least about 20 percent, at least about 40 percent, or at least about 60 percent less than the carbon dioxide concentration present in the hydrocarbon feed stream  200 . The carbon dioxide-lean stream  234  may also contain a reduced concentration of C 3+  compared to the hydrocarbon feed stream  200 . In various embodiments, the carbon dioxide-lean stream  234  comprises less than about 5 percent, less than about 1 percent, or is substantially free of C 3+ . In yet other embodiments, the C 3+  concentration in the carbon dioxide-lean stream  234  is at least about 20 percent, at least about 40 percent, or at least about 60 percent less than the C 3+  concentration present in the hydrocarbon feed stream  200 . Finally, in other embodiments, the carbon dioxide-lean stream  234  contains at least about 90 percent, at least about 98 percent, or at least about 99 percent of a combination of methane and carbon dioxide. 
     The heavy hydrocarbon streams  212 ,  252 ,  254  may contain a mixture of heavy hydrocarbons and some other compounds. Specifically, the composition of the heavy hydrocarbon streams  212 ,  252 ,  254  contains an increased C 3+  concentration and a decreased methane concentration, ethane, and carbon dioxide compared to the hydrocarbon feed stream  200 . In embodiments, the heavy hydrocarbon streams  212 ,  252 ,  254  comprises at least about 90 percent, at least about 95 percent, or at least about 99 percent C 3+ . In other embodiments, the heavy hydrocarbon streams  212 ,  252 ,  254  comprises less than about 5 percent, less than about 1 percent, or is substantially free of methane and/or ethane. In yet other embodiments, the heavy hydrocarbon streams  212 ,  252 ,  254  contains less than about 10 percent, less than about 5 percent, or less than about 1 percent of the carbon dioxide. Alternatively, the heavy hydrocarbon streams  212 ,  252 ,  254  comprises at least about 20 percent, at least about 40 percent, or at least about 60 percent less carbon dioxide than the hydrocarbon feed stream  200 . In an embodiment, the heavy hydrocarbon streams  212 ,  252 ,  254  described herein are suitable for use or sale as natural gas liquids (NGL). 
     The carbon dioxide-rich stream  244  described herein may comprise a mixture of hydrocarbons and carbon dioxide. Specifically, the carbon dioxide-rich stream  244  contains a decreased concentration of hydrocarbons and an increased carbon dioxide concentration compared to the hydrocarbon feed stream  200 . In various embodiments, the carbon dioxide-rich stream  244  comprises less than about 10 percent, less than about 5 percent, or is substantially free of hydrocarbons. In other embodiments, the carbon dioxide-rich stream  244  contains at least about 80 percent, at least about 90 percent, or at least about 95 percent of the carbon dioxide. The carbon dioxide-rich stream  244  described herein may be vented, transported, sold, or used for other purposes including reinjection into a subterranean formation. 
     The acid gas stream  250  described herein may comprise a mixture of hydrocarbons and at least one acid gas, such as H 2 S or carbon dioxide. Specifically, the composition of the acid gas stream  250  may contain a decreased hydrocarbon concentration and an increased acid gas concentration compared to the hydrocarbon feed stream  200 . In various embodiments, the acid gas stream  250  comprises less than about 10 percent, less than about 5 percent, or is substantially free of hydrocarbons. In other embodiments, the acid gas stream  250  contains at least about 90 percent, at least about 95 percent, or at least about 99 percent of the acid gas. The acid gas stream  250  described herein may be vented, sold, reinjected, or otherwise disposed of as desired. 
     Although the hydrocarbon sweetening process  130  may be any sweetening process, in one embodiment the hydrocarbon sweetening process  130  is a physical solvent process. The physical solvent process sweetens the hydrocarbon stream by using an organic solvent to absorb the carbon dioxide from the hydrocarbon stream. Examples of these physical solvents include SELEXOL®, RECTISOL®, PURISOL®, and FLUOR® solvents such as propylene carbonate. The physical solvent process begins by contacting the carbon dioxide-lean stream  234  with the solvent at high pressure. The solvent absorbs the carbon dioxide such that subsequent separation of the solvent from the hydrocarbons produces a hydrocarbon stream with a relatively low carbon dioxide concentration. The carbon dioxide-loaded solvent is then regenerated by lowering the pressure of the solvent, typically through a series of flash drums, which causes the carbon dioxide to separate from the solvent. The solvent is then compressed and recycled into the hydrocarbon stream, while the carbon dioxide is vented or sold. 
     Alternatively, the hydrocarbon sweetening process  130  may be a membrane separation process. Membrane separation processes use membranes to separate carbon dioxide from the carbon dioxide-lean stream  234  at the molecular level. Specifically, the pores in the membranes are sized to allow carbon dioxide to pass through the membrane and form a permeate gas, while the larger hydrocarbon molecules bypass the membrane and form a residue gas. Depending on the composition of the hydrocarbons, this configuration may be reversed such that the carbon dioxide forms the residue gas and the hydrocarbons form the permeate gas. Because the membrane process is dependent on, among other factors, the composition of the hydrocarbons, the selection of the pore size is best determined by persons of ordinary skill in the art. 
     In yet another embodiment, the hydrocarbon sweetening process  130  may be a carbon dioxide recovery process. One example of a suitable carbon dioxide recovery process is the Ryan-Holmes process. The Ryan-Holmes process uses a solvent and a plurality of columns to separate the carbon dioxide-lean stream  234  into a carbon dioxide-rich stream, a methane-rich stream, an ethane-rich stream, and a heavy hydrocarbon stream. The columns may include a demethanizer, a carbon dioxide recovery unit, a propane recovery unit, and a solvent recovery unit. The columns are arranged in series with the solvent being recycled to the first column in the series. The specific arrangement of the various columns depends on the composition of the feed hydrocarbon stream and is best determined by persons of ordinary skill in the art. Finally, persons of ordinary skill in the art will appreciate that the hydrocarbon sweetening process  130  may be a process other than the exemplary processes described herein. 
     When the carbon dioxide fractionalization process  100  is implemented prior to a hydrocarbon sweetening process  130 , the processing capacity of the hydrocarbon sweetening process  130  is increased. Specifically, the processing capacity of the hydrocarbon sweetening process  130  may be directly proportional to the decrease in carbon dioxide concentration between the hydrocarbon feed stream  200  and the carbon dioxide-lean stream  234 . For example, if the carbon dioxide concentration of the carbon dioxide-lean stream  234  is half of the carbon dioxide concentration of the hydrocarbon feed stream  200 , then the processing capacity of the hydrocarbon sweetening process  130  is doubled. In addition, the processing capacity of the hydrocarbon sweetening process  130  may be directly proportional to the decrease in flow rate between the hydrocarbon feed stream  200  and the carbon dioxide-lean stream  234 . For example, if the flow rate of the carbon dioxide-lean stream  234  is half of the flow rate of the hydrocarbon feed stream  200 , then the processing capacity of the hydrocarbon sweetening process  130  is also doubled. The two affects may also be cumulative such that if the carbon dioxide concentration of the carbon dioxide-lean stream  234  is half of the carbon dioxide concentration of the hydrocarbon feed stream  200  and the flow rate of the carbon dioxide-lean stream  234  is half of the flow rate of the hydrocarbon feed stream  200 , then the processing capacity of the hydrocarbon sweetening process  130  is increased by a factor of four. 
     The separators  106 ,  108 ,  120 ,  134  may be any of a variety of process equipment suitable for separating a stream into two separate streams having different compositions, states, temperatures, and/or pressures. For example, one or more of the separators  106 ,  108 ,  120 ,  134  may be a column having trays, packing, or some other type of complex internal structure. Examples of such columns include scrubbers, strippers, absorbers, adsorbers, packed columns, and distillation columns having valve, sieve, or other types of trays. Such columns may employ weirs, downspouts, internal baffles, temperature, and/or pressure control elements. Such columns may also employ some combination of reflux condensers and/or reboilers, including intermediate stage condensers and reboilers. Alternatively, one or more of the separators  106 ,  108 ,  120 ,  134  may be a phase separator. A phase separator is a vessel that separates an inlet stream into a substantially vapor stream and a substantially liquid stream, such as a knock-out drum or a flash drum. Such vessels may have some internal baffles, temperature, and/or pressure control elements, but generally lack any trays or other type of complex internal structure commonly found in columns. Finally, one or more of the separators  106 ,  108 ,  120 ,  134  may be any other type of separator, such as a membrane separator. 
     The reboilers  110 ,  124  and condensers  122 ,  132  described herein may be any of a variety of process equipment suitable for changing the temperature and/or separating any of the streams described herein. In embodiments, the reboilers  110 ,  124  and the condensers  122 ,  132  may be any vessel that separates an inlet stream into a substantially vapor stream and a substantially liquid stream. These vessels typically have some internal baffles, temperature, and/or pressure control elements, but generally lack any trays or other type of complex internal structure found in other vessels. In specific embodiments, heat exchangers and kettle-type reboilers may be used as the reboilers  110 ,  124  and condensers  122 ,  132  described herein. 
     The heat exchangers  102 ,  104 ,  114 ,  118 ,  126  described herein may be any of a variety of process equipment suitable for heating or cooling any of the streams described herein. Generally, heat exchangers  102 ,  104 ,  114 ,  118 ,  126  are relatively simple devices that allow heat to be exchanged between two fluids without the fluids directly contacting each other. In the case of an air cooler, one of the fluids is atmospheric air, which may be forced over tubes or coils using one or more fans. The types of heat exchangers  102 ,  104 ,  114 ,  118 ,  126  suitable for use with the carbon dioxide fractionalization process  100  include shell and tube, kettle-type, air cooled, hairpin, bayonet, and plate-fin heat exchangers. 
     The compressor  112  and pump  128  described herein may be any of a variety of process equipment suitable for increasing the pressure, temperature, and/or density of any of the streams described herein. Generally, compressors are associated with vapor streams and pumps are associated with liquid streams; however such a limitation should not be read into the present processes as the compressors and pumps described herein may be interchangeable based upon the specific conditions and compositions of the streams. The types of compressors and pumps suitable for the uses described herein include centrifugal, axial, positive displacement, rotary, and reciprocating compressors and pumps. Finally, the carbon dioxide fractionalization process  100  may contain additional compressors and/or pumps other than those described herein. 
     The mixer  116  described herein may either be a dynamic mixer or a static mixer. Dynamic mixers are mixers that employ motion or mechanical agitation to mix two or more streams. For example, a dynamic mixer may be a tank with a paddle operating either in a continuous or batch mode. In contrast, static mixers are mixers that do not employ any motion or mechanical agitation to mix two or more streams. For example, a static mixer may be a convergence of piping designed to combine two streams, such as a pipe tee. Either type of mixer may be configured with internal baffles to promote the mixing of the feed streams. 
     The energy streams  300 ,  302 ,  304 ,  306 ,  308 ,  310 ,  312 ,  314  described herein may be derived from any number of suitable sources. For example, heat may be added to a process stream using steam, turbine exhaust, or some other hot fluid and a heat exchanger. Similarly, heat may be removed from a process stream by using a refrigerant, air, or some other cold fluid and a heat exchanger. Further, electrical energy can be supplied to compressors, pumps, and other mechanical equipment to increase the pressure or other physical properties of a fluid. Similarly, turbines, generators, or other mechanical equipment can be used to extract physical energy from a stream and optionally convert the physical energy into electrical energy. Persons of ordinary skill in the art are aware of how to configure the processes described herein with the required energy streams  300 ,  302 ,  304 ,  306 ,  308 ,  310 ,  312 ,  314 . In addition, persons of ordinary skill in the art will appreciate that the carbon dioxide fractionalization process  100  may contain additional equipment, process steams, and/or energy streams other than those described herein. 
     The carbon dioxide fractionalization process  100  described herein has many advantages. One advantage is that it purifies a hydrocarbon stream used by one of the hydrocarbon sweetening processes  130  described above. Specifically, the carbon dioxide fractionalization process  100  purifies the hydrocarbon stream by removing some of the carbon dioxide and C 3+  from the hydrocarbon stream. The purification of the hydrocarbon stream improves the performance of the hydrocarbon sweetening process  130  by reducing the carbon dioxide and C 3+  loading on the hydrocarbon sweetening process  130 . The reduction in loading increases the processing capacity for the hydrocarbon sweetening process  130 , which is particularly advantageous for existing processing facilities. Moreover, the addition of the carbon dioxide fractionalization process  100  to existing hydrocarbon sweetening processes  130  may reduce the energy requirements of the combined processes. Specifically, the carbon dioxide fractionalization process  100  liquefies some of the carbon dioxide and C 3+  in the hydrocarbon feed and feeds the carbon dioxide-lean stream  234  to the sweetening process  130 , thereby reducing the compression requirements within the hydrocarbon sweetening process  130 . The reduction in compression requirements may decrease the total energy requirements of the two processes per unit amount of hydrocarbons, e.g. Btu/SCF (British thermal units per standard cubic foot of gas). Other advantages will be apparent to persons of ordinary skill in the art. 
     EXAMPLES 
     In one example, a process simulation was performed using the carbon dioxide fractionalization process  100  shown in  FIG. 1 . The simulation was performed using the Hyprotech Ltd. HYSYS Process v2.1.1 (Build 3198) software package. The carbon dioxide fractionalization process  100  separated a West Texas hydrocarbon feed containing about 63 percent carbon dioxide into a carbon dioxide-lean stream  234  containing about 43 percent carbon dioxide, a carbon dioxide-rich stream  244  containing about 95 percent carbon dioxide, an acid gas stream  250  containing about 100 percent carbon dioxide and trace amounts of other acid gases, and a heavy hydrocarbon stream containing about 99 percent C 3+ . It is notable that the process produces 454 gallons per minute of pipeline-grade liquefied carbon dioxide. The carbon dioxide produced by a SELEXOL® plant without this process produces a similar amount of gaseous carbon dioxide, but at atmospheric pressure or at a vacuum. The compression requirements for such a gaseous carbon dioxide stream are large, e.g. 25,000 BTU per thousand standard cubic feet (MSCF), and are generally cost prohibitive. Thus, the present process allows carbon dioxide to be economically recovered and reused, unlike the prior processes. The material streams, their compositions, and the associated energy streams produced by the simulation are provided in tables 1, 2, and 3 below. The specified values are indicated by an asterisk (*). The physical properties are provided in degrees Fahrenheit (F), pounds per square inch gauge (psig), million standard cubic feet per day (MMSCFD), pounds per hour (lb/hr), U.S. gallons per minute (USGPM), and British thermal units per hour (Btu/hr). 
     
       
         
           
               
             
               
                 TABLE 1A 
               
             
            
               
                   
               
               
                 Material Streams 
               
            
           
           
               
               
               
               
               
            
               
                 Name 
                 200 
                 248 
                 202 
                 224 
               
               
                   
               
            
           
           
               
               
               
               
               
            
               
                 Vapor Fraction 
                 1.0000 
                 1.0000 
                 1.0000 
                 1.0000 
               
               
                 Temperature 
                 100.0* 
                 −15.92 
                 99.00* 
                 60.00* 
               
               
                 (F.) 
               
               
                 Pressure (psig) 
                 485.3* 
                 385.3 
                 480.3 
                 980.3 
               
               
                 Molar Flow 
                 100.0* 
                 99.82 
                 100.0 
                 99.82 
               
               
                 (MMSCFD) 
               
               
                 Mass Flow 
                  3.731e+05 
                  3.713e+05 
                  3.731e+05 
                  3.713e+05 
               
               
                 (lb/hr) 
               
               
                 Liquid 
                 1176 
                 1171 
                 1176 
                 1171 
               
               
                 Volume Flow 
               
               
                 (USGPM) 
               
               
                 Heat Flow 
                 −1.305e+09 
                 −1.316e+09 
                 −1.305e+09 
                 −1.315e+09 
               
               
                 (Btu/hr) 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 1B 
               
             
            
               
                   
               
               
                 Material Streams 
               
            
           
           
               
               
               
               
               
            
               
                 Name 
                 230 
                 240 
                 232 
                 234 
               
               
                   
               
            
           
           
               
               
               
               
               
            
               
                 Vapor Fraction 
                 1.0000 
                 0.0000 
                 1.0000 
                 1.0000 
               
               
                 Temperature 
                 −5.769 
                 65.16 
                 92.33 
                 92.78 
               
               
                 (F.) 
               
               
                 Pressure (psig) 
                 925.3 
                 935.3 
                 920.3 
                 915.3 
               
               
                 Molar Flow 
                 61.13 
                 38.68 
                 61.13 
                 61.13 
               
               
                 (MMSCFD) 
               
               
                 Mass Flow 
                  1.896e+05 
                  1.817e+05 
                  1.896e+05 
                  1.896e+05 
               
               
                 (lb/hr) 
               
               
                 Liquid 
                 716.7 
                 454.5 
                 716.7 
                 716.7 
               
               
                 Volume Flow 
               
               
                 (USGPM) 
               
               
                 Heat Flow 
                 −6.242e+08 
                 −7.078e+08 
                 −6.145e+08 
                 −6.145e+08 
               
               
                 (Btu/hr) 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 1C 
               
             
            
               
                   
               
               
                 Material Streams 
               
            
           
           
               
               
               
               
               
            
               
                 Name 
                 244 
                 242 
                 218 
                 212 
               
               
                   
               
            
           
           
               
               
               
               
               
            
               
                 Vapor Fraction 
                   0.0000 
                 0.0000 
                 1.0000 
                 0.0000 
               
               
                 Temperature 
                 72.39 
                 55.00 
                 123.3 
                 264.0 
               
               
                 (F.) 
               
               
                 Pressure (psig) 
                 1785*    
                 930.3 
                 985.3* 
                 395.3 
               
               
                 Molar Flow 
                 38.68 
                 38.68 
                 99.82 
                 0.1832 
               
               
                 (MMSCFD) 
               
               
                 Mass Flow 
                  1.817e+05 
                  1.817e+05 
                  3.713e+05 
                 1801 
               
               
                 (lb/hr) 
               
               
                 Liquid 
                 454.5  
                 454.5 
                 1171 
                 5.233 
               
               
                 Volume Flow 
               
               
                 (USGPM) 
               
               
                 Heat Flow 
                 −7.092e+08 
                 −7.100e+08 
                 −1.306e+09 
                 −1.905e+06 
               
               
                 (Btu/hr) 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 1D 
               
             
            
               
                   
               
               
                 Material Streams 
               
            
           
           
               
               
            
               
                   
                 Name 
               
            
           
           
               
               
               
               
            
               
                   
                 250 
                 252 
                 254 
               
               
                   
                   
               
            
           
           
               
               
               
               
               
            
               
                 Vapor 
                   
                 1.0000 
                 0.0000 
                 0.0000 
               
               
                 Fraction 
               
               
                 Tem- 
                 (F.) 
                 100.0* 
                 265.2* 
                 120.0* 
               
               
                 perature 
               
               
                 Pressure 
                 (psig) 
                 485.3* 
                 485.3* 
                 465.3* 
               
               
                 Molar 
                 (MMSCFD) 
                 0.02473 
                 0.1585 
                 0.1585 
               
               
                 Flow 
               
               
                 Mass 
                 (lb/hr) 
                 119.5 
                 1682 
                 1682 
               
               
                 Flow 
               
               
                 Liquid 
                 (USGPM) 
                 0.2892 
                 4.944 
                 4.944 
               
               
                 Volume 
               
               
                 Flow 
               
               
                 Heat Flow 
                 (Btu/hr) 
                 −4.610e+05 
                 −1.444e+06 
                 −1.593e+06 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 2A 
               
             
            
               
                   
               
               
                 Stream Compositions 
               
            
           
           
               
               
            
               
                   
                 Name 
               
            
           
           
               
               
               
               
               
            
               
                   
                 200 
                 248 
                 202 
                 224 
               
               
                   
                   
               
            
           
           
               
               
               
               
               
            
               
                 Comp Mole Frac (H2S) 
                 0.0000* 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (Nitrogen) 
                 0.0051* 
                 0.0051 
                 0.0051 
                 0.0051 
               
               
                 Comp Mole Frac (CO2) 
                 0.6308* 
                 0.6317 
                 0.6308 
                 0.6317 
               
               
                 Comp Mole Frac (Methane) 
                 0.3570* 
                 0.3577 
                 0.3570 
                 0.3577 
               
               
                 Comp Mole Frac (Ethane) 
                 0.0037* 
                 0.0037 
                 0.0037 
                 0.0037 
               
               
                 Comp Mole Frac (Propane) 
                 0.0013* 
                 0.0013 
                 0.0013 
                 0.0013 
               
               
                 Comp Mole Frac (i-Butane) 
                 0.0002* 
                 0.0002 
                 0.0002 
                 0.0002 
               
               
                 Comp Mole Frac (n-Butane) 
                 0.0005* 
                 0.0004 
                 0.0005 
                 0.0004 
               
               
                 Comp Mole Frac (i-Pentane) 
                 0.0000* 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (n-Pentane) 
                 0.0000* 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (n-Hexane) 
                 0.0007* 
                 0.0000 
                 0.0007 
                 0.0000 
               
               
                 Comp Mole Frac (n-Octane) 
                 0.0008* 
                 0.0000 
                 0.0008 
                 0.0000 
               
               
                 Comp Mole Frac (H2O) 
                 0.0000* 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 2B 
               
             
            
               
                   
               
               
                 Stream Compositions 
               
            
           
           
               
               
            
               
                   
                 Name 
               
            
           
           
               
               
               
               
               
            
               
                   
                 230 
                 240 
                 232 
                 234 
               
               
                   
                   
               
            
           
           
               
               
               
               
               
            
               
                 Comp Mole Frac (H2S) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (Nitrogen) 
                 0.0083 
                 0.0001 
                 0.0083 
                 0.0083 
               
               
                 Comp Mole Frac (CO2) 
                 0.4303 
                 0.9500 
                 0.4303 
                 0.4303 
               
               
                 Comp Mole Frac (Methane) 
                 0.5568 
                 0.0430 
                 0.5568 
                 0.5568 
               
               
                 Comp Mole Frac (Ethane) 
                 0.0041 
                 0.0031 
                 0.0041 
                 0.0041 
               
               
                 Comp Mole Frac (Propane) 
                 0.0005 
                 0.0025 
                 0.0005 
                 0.0005 
               
               
                 Comp Mole Frac (i-Butane) 
                 0.0000 
                 0.0004 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (n-Butane) 
                 0.0000 
                 0.0010 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (i-Pentane) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (n-Pentane) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (n-Hexane) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (n-Octane) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (H2O) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 2C 
               
             
            
               
                   
               
               
                 Stream Compositions 
               
            
           
           
               
               
            
               
                   
                 Name 
               
            
           
           
               
               
               
               
               
            
               
                   
                 244 
                 242 
                 218 
                 212 
               
               
                   
                   
               
            
           
           
               
               
               
               
               
            
               
                 Comp Mole Frac (H2S) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (Nitrogen) 
                 0.0001 
                 0.0001 
                 0.0051 
                 0.0000 
               
               
                 Comp Mole Frac (CO2) 
                 0.9500 
                 0.9500 
                 0.6317 
                 0.1350 
               
               
                 Comp Mole Frac (Methane) 
                 0.0430 
                 0.0430 
                 0.3577 
                 0.0001 
               
               
                 Comp Mole Frac (Ethane) 
                 0.0031 
                 0.0031 
                 0.0037 
                 0.0050 
               
               
                 Comp Mole Frac (Propane) 
                 0.0025 
                 0.0025 
                 0.0013 
                 0.0142 
               
               
                 Comp Mole Frac (i-Butane) 
                 0.0004 
                 0.0004 
                 0.0002 
                 0.0078 
               
               
                 Comp Mole Frac (n-Butane) 
                 0.0010 
                 0.0010 
                 0.0004 
                 0.0472 
               
               
                 Comp Mole Frac (i-Pentane) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (n-Pentane) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (n-Hexane) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.3813 
               
               
                 Comp Mole Frac (n-Octane) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.4094 
               
               
                 Comp Mole Frac (H2O) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 2D 
               
             
            
               
                   
               
               
                 Stream Compositions 
               
            
           
           
               
               
            
               
                   
                 Name 
               
            
           
           
               
               
               
               
            
               
                   
                 250 
                 252 
                 254 
               
               
                   
                   
               
            
           
           
               
               
               
               
               
            
               
                   
                 Comp Mole Frac (H2S) 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                   
                 Comp Mole Frac (Nitrogen) 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                   
                 Comp Mole Frac (CO2) 
                 1.0000 
                 0.0000 
                 0.0000 
               
               
                   
                 Comp Mole Frac (Methane) 
                 0.0000 
                 0.0001 
                 0.0001 
               
               
                   
                 Comp Mole Frac (Ethane) 
                 0.0000 
                 0.0058 
                 0.0058 
               
               
                   
                 Comp Mole Frac (Propane) 
                 0.0000 
                 0.0164 
                 0.0164 
               
               
                   
                 Comp Mole Frac (i-Butane) 
                 0.0000 
                 0.0090 
                 0.0090 
               
               
                   
                 Comp Mole Frac (n-Butane) 
                 0.0000 
                 0.0545 
                 0.0545 
               
               
                   
                 Comp Mole Frac (i-Pentane) 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                   
                 Comp Mole Frac (n-Pentane) 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                   
                 Comp Mole Frac (n-Hexane) 
                 0.0000 
                 0.4408 
                 0.4408 
               
               
                   
                 Comp Mole Frac (n-Octane) 
                 0.0000 
                 0.4733 
                 0.4733 
               
               
                   
                 Comp Mole Frac (H2O) 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                   
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 3 
               
             
            
               
                   
               
               
                 Energy Streams 
               
            
           
           
               
               
               
            
               
                   
                 Name 
                 HeatFlow (Btu/hr) 
               
               
                   
                   
               
               
                   
                 308 
                 8.518e+06 
               
               
                   
                 302 
                 3.623e+05 
               
               
                   
                 304 
                 1.027e+07 
               
               
                   
                 306 
                 2.505e+07 
               
               
                   
                 314 
                 7.719e+05 
               
               
                   
                 310 
                 2.184e+06 
               
               
                   
                 312 
                 1.293e+07 
               
               
                   
                   
               
            
           
         
       
     
     In another example, a process simulation was performed using the carbon dioxide fractionalization process  100  shown in  FIG. 2 . The simulation was performed using the Hyprotech Ltd. HYSYS Process v2.1.1 (Build 3198) software package. The carbon dioxide fractionalization process  100  separated a West Texas hydrocarbon feed containing about 63 percent carbon dioxide into a carbon dioxide-lean stream  234  containing about 36 percent carbon dioxide, a carbon dioxide-rich stream  244  containing about 95 percent carbon dioxide, and a heavy hydrocarbon stream containing about 93 percent C 3+ . The material streams, their compositions, and the associated energy streams produced by the simulation are provided in tables 4, 5, and 6 below. 
     
       
         
           
               
             
               
                 TABLE 4A 
               
             
            
               
                   
               
               
                 Material Streams 
               
            
           
           
               
               
            
               
                   
                 Name 
               
            
           
           
               
               
               
               
               
            
               
                   
                 200 
                 204 
                 206 
                 222 
               
               
                   
                   
               
            
           
           
               
               
               
               
               
               
            
               
                 Vapor Fraction 
                   
                 1.0000 
                 0.8205 
                 0.0000 
                 1.0000 
               
               
                 Temperature 
                 (F.) 
                 100.0* 
                 22.00* 
                 22.00 
                 34.23 
               
               
                 Pressure 
                 (psig) 
                 945.3* 
                 935.3 
                 935.3 
                 935.3 
               
               
                 Molar Flow 
                 (MMSCFD) 
                 300.0* 
                 300.0 
                 53.85 
                 299.6 
               
               
                 Mass Flow 
                 (lb/hr) 
                 1.119e+06 
                 1.119e+06 
                 2.343e+05 
                 1.115e+06 
               
               
                 Liquid Volume Flow 
                 (USGPM) 
                 3529 
                 3529 
                 640.1 
                 3516 
               
               
                 Heat Flow 
                 (Btu/hr) 
                 −3.932e+09 
                 −3.988e+09 
                 −8.836e+08 
                 −3.961e+09 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 4B 
               
             
            
               
                   
               
               
                 Material Streams 
               
            
           
           
               
               
            
               
                   
                 Name 
               
            
           
           
               
               
               
               
               
            
               
                   
                 214 
                 212 
                 202 
                 218 
               
               
                   
                   
               
            
           
           
               
               
               
               
               
               
            
               
                 Vapor Fraction 
                   
                 1.0000 
                 0.0000 
                 1.0000 
                 1.0000 
               
               
                 Temperature 
                 (F.) 
                 −5.027 
                 335.1 
                 47.95 
                 100.0* 
               
               
                 Pressure 
                 (psig) 
                 335.3 
                 340.3 
                 940.3 
                 960.3* 
               
               
                 Molar Flow 
                 (MMSCFD) 
                 53.41 
                 0.4397 
                 300.0 
                 53.41 
               
               
                 Mass Flow 
                 (lb/hr) 
                 2.299e+05 
                 4409 
                 1.119e+06 
                 2.299e+05 
               
               
                 Liquid Volume Flow 
                 (USGPM) 
                 627.1 
                 12.95 
                 3529 
                 627.1 
               
               
                 Heat Flow 
                 (Btu/hr) 
                 −8.582e+08 
                 −4.030e+06 
                 −3.957e+09 
                 −8.564e+08 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 4C 
               
             
            
               
                   
               
               
                 Material Streams 
               
            
           
           
               
               
            
               
                   
                 Name 
               
            
           
           
               
               
               
               
               
            
               
                   
                 224 
                 230 
                 240 
                 232 
               
               
                   
                   
               
            
           
           
               
               
               
               
               
               
            
               
                 Vapor Fraction 
                   
                 1.0000 
                 1.0000 
                 0.00000 
                 1.0000 
               
               
                 Temperature 
                 (F.) 
                 32.00* 
                 −20.00 
                 61.65 
                 −17.19 
               
               
                 Pressure 
                 (psig) 
                 930.3 
                 895.3 
                 900.3 
                 890.3 
               
               
                 Molar Flow 
                 (MMSCFD) 
                 299.6 
                 161.3 
                 138.3 
                 161.3 
               
               
                 Mass Flow 
                 (lb/hr) 
                 1.115e+06 
                 4.649e+05 
                 6.501e+05 
                 4.649e+05 
               
               
                 Liquid Volume Flow 
                 (USGPM) 
                 3516 
                 1890 
                 1626 
                 1890 
               
               
                 Heat Flow 
                 (Btu/hr) 
                 −3.962e+09 
                 −1.473e+09 
                 −2.533e+09 
                 −1.472e+09 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 4D 
               
             
            
               
                   
               
               
                 Material Streams 
               
            
           
           
               
               
            
               
                   
                 Name 
               
            
           
           
               
               
               
               
               
               
            
               
                   
                 234 
                 244 
                 242 
                 220 
                 216 
               
               
                   
                   
               
            
           
           
               
               
               
               
               
               
               
            
               
                 Vapor Fraction 
                   
                 1.0000 
                 0.0000  
                 0.0000 
                 1.0000 
                 1.0000 
               
               
                 Temperature 
                 (F.) 
                 85.00* 
                 73.48    
                 55.00* 
                 22.00 
                 155.2 
               
               
                 Pressure 
                 (psig) 
                 885.3 
                 1785*      
                 895.3 
                 935.3 
                 965.3 
               
               
                 Molar Flow 
                 (MMSCFD) 
                 161.3 
                 138.3     
                 138.3 
                 246.2 
                 53.41 
               
               
                 Mass Flow 
                 (lb/hr) 
                 4.649e+05 
                  6.501e+05 
                 6.501e+05 
                 8.851e+05 
                 2.299e+05 
               
               
                 Liquid Volume Flow 
                 (USGPM) 
                 1890 
                 1626       
                 1626 
                 2889 
                 627.1 
               
               
                 Heat Flow 
                 (Btu/hr) 
                 −1.446e+09 
                 −2.535e+09 
                 −2.538e+09 
                 −3.105e+09 
                 −8.518e+08 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 5A 
               
             
            
               
                   
               
               
                 Stream Compositions 
               
            
           
           
               
               
            
               
                   
                 Name 
               
            
           
           
               
               
               
               
               
            
               
                   
                 200 
                 204 
                 206 
                 220 
               
               
                   
                   
               
            
           
           
               
               
               
               
               
            
               
                 Comp Mole Frac (H2S) 
                 0.0000* 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (Nitrogen) 
                 0.0051* 
                 0.0051 
                 0.0016 
                 0.0051 
               
               
                 Comp Mole Frac (CO2) 
                 0.6308* 
                 0.6308 
                 0.8168 
                 0.6316 
               
               
                 Comp Mole Frac (Methane) 
                 0.3570* 
                 0.3570 
                 0.1680 
                 0.3576 
               
               
                 Comp Mole Frac (Ethane) 
                 0.0037* 
                 0.0037 
                 0.0037 
                 0.0037 
               
               
                 Comp Mole Frac (Propane) 
                 0.0013* 
                 0.0013 
                 0.0020 
                 0.0013 
               
               
                 Comp Mole Frac (i-Butane) 
                 0.0002* 
                 0.0002 
                 0.0004 
                 0.0001 
               
               
                 Comp Mole Frac (n-Butane) 
                 0.0005* 
                 0.0005 
                 0.0011 
                 0.0003 
               
               
                 Comp Mole Frac (i-Pentane) 
                 0.0000* 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (n-Pentane) 
                 0.0000* 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (n-Hexane) 
                 0.0007* 
                 0.0007 
                 0.0028 
                 0.0002 
               
               
                 Comp Mole Frac (n-Octane) 
                 0.0008* 
                 0.0008 
                 0.0037 
                 0.0001 
               
               
                 Comp Mole Frac (H2O) 
                 0.0000* 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 5B 
               
             
            
               
                   
               
               
                 Stream Compositions 
               
            
           
           
               
               
            
               
                   
                 Name 
               
            
           
           
               
               
               
               
               
            
               
                   
                 214 
                 212 
                 202 
                 218 
               
               
                   
                   
               
            
           
           
               
               
               
               
               
            
               
                 Comp Mole Frac (H2S) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (Nitrogen) 
                 0.0016 
                 0.0000 
                 0.0051 
                 0.0016 
               
               
                 Comp Mole Frac (CO2) 
                 0.8229 
                 0.0700 
                 0.6308 
                 0.8229 
               
               
                 Comp Mole Frac (Methane) 
                 0.1693 
                 0.0000 
                 0.3570 
                 0.1693 
               
               
                 Comp Mole Frac (Ethane) 
                 0.0037 
                 0.0000 
                 0.0037 
                 0.0037 
               
               
                 Comp Mole Frac (Propane) 
                 0.0018 
                 0.0302 
                 0.0013 
                 0.0018 
               
               
                 Comp Mole Frac (i-Butane) 
                 0.0001 
                 0.0252 
                 0.0002 
                 0.0001 
               
               
                 Comp Mole Frac (n-Butane) 
                 0.0003 
                 0.0949 
                 0.0005 
                 0.0003 
               
               
                 Comp Mole Frac (i-Pentane) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (n-Pentane) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (n-Hexane) 
                 0.0001 
                 0.3260 
                 0.0007 
                 0.0001 
               
               
                 Comp Mole Frac (n-Octane) 
                 0.0000 
                 0.4537 
                 0.0008 
                 0.0000 
               
               
                 Comp Mole Frac (H2O) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 5C 
               
             
            
               
                   
               
               
                 Stream Compositions 
               
            
           
           
               
               
            
               
                   
                 Name 
               
            
           
           
               
               
               
               
               
            
               
                   
                 224 
                 230 
                 240 
                 232 
               
               
                   
                   
               
            
           
           
               
               
               
               
               
            
               
                 Comp Mole Frac (H2S) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (Nitrogen) 
                 0.0051 
                 0.0094 
                 0.0000 
                 0.0094 
               
               
                 Comp Mole Frac (CO2) 
                 0.6316 
                 0.3586 
                 0.9500 
                 0.3586 
               
               
                 Comp Mole Frac (Methane) 
                 0.3576 
                 0.6275 
                 0.0428 
                 0.6275 
               
               
                 Comp Mole Frac (Ethane) 
                 0.0037 
                 0.0041 
                 0.0032 
                 0.0041 
               
               
                 Comp Mole Frac (Propane) 
                 0.0013 
                 0.0004 
                 0.0023 
                 0.0004 
               
               
                 Comp Mole Frac (i-Butane) 
                 0.0001 
                 0.0000 
                 0.0003 
                 0.0000 
               
               
                 Comp Mole Frac (n-Butane) 
                 0.0003 
                 0.0000 
                 0.0007 
                 0.0000 
               
               
                 Comp Mole Frac (i-Pentane) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (n-Pentane) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac (n-Hexane) 
                 0.0002 
                 0.0000 
                 0.0005 
                 0.0000 
               
               
                 Comp Mole Frac (n-Octane) 
                 0.0001 
                 0.0000 
                 0.0002 
                 0.0000 
               
               
                 Comp Mole Frac (H2O) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 5D 
               
             
            
               
                   
               
               
                 Stream Compositions 
               
            
           
           
               
               
            
               
                   
                 Name 
               
            
           
           
               
               
               
               
               
               
            
               
                   
                 234 
                 244 
                 242 
                 220 
                 216 
               
               
                   
                   
               
            
           
           
               
               
               
               
               
               
            
               
                 Comp Mole Frac (H2S) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 Comp Mole Frac 
                 0.0094 
                 0.0000 
                 0.0000 
                 0.0059 
                 0.0016 
               
               
                 (Nitrogen) 
               
               
                 Comp Mole Frac (CO2) 
                 0.3586 
                 0.9500 
                 0.9500 
                 0.5901 
                 0.8229 
               
               
                 Comp Mole Frac 
                 0.6275 
                 0.0428 
                 0.0428 
                 0.3984 
                 0.1693 
               
               
                 (Methane) 
               
               
                 Comp Mole Frac 
                 0.0041 
                 0.0032 
                 0.0032 
                 0.0037 
                 0.0037 
               
               
                 (Ethane) 
               
               
                 Comp Mole Frac 
                 0.0004 
                 0.0023 
                 0.0023 
                 0.0011 
                 0.0018 
               
               
                 (Propane) 
               
               
                 Comp Mole Frac 
                 0.0000 
                 0.0003 
                 0.0003 
                 0.0001 
                 0.0001 
               
               
                 (i-Butane) 
               
               
                 Comp Mole Frac 
                 0.0000 
                 0.0007 
                 0.0007 
                 0.0003 
                 0.0003 
               
               
                 (n-Butane) 
               
               
                 Comp Mole Frac 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 (i-Pentane) 
               
               
                 Comp Mole Frac 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                 (n-Pentane) 
               
               
                 Comp Mole Frac 
                 0.0000 
                 0.0005 
                 0.0005 
                 0.0002 
                 0.0001 
               
               
                 (n-Hexane) 
               
               
                 Comp Mole Frac 
                 0.0000 
                 0.0002 
                 0.0002 
                 0.0001 
                 0.0000 
               
               
                 (n-Octane) 
               
               
                 Comp Mole Frac (H2O) 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
                 0.0000 
               
               
                   
               
            
           
         
       
     
     
       
         
           
               
             
               
                 TABLE 6 
               
             
            
               
                   
               
               
                 Energy Streams 
               
            
           
           
               
               
               
            
               
                   
                   
                 Heat Flow 
               
               
                   
                 Name 
                 (Btu/hr) 
               
               
                   
                   
               
               
                   
                 300 
                 3.107e+07 
               
               
                   
                 302 
                 2.138e+07 
               
               
                   
                 304 
                 6.401e+06 
               
               
                   
                 306 
                 7.371e+07 
               
               
                   
                 308 
                 3.014e+07 
               
               
                   
                 314 
                 2.890e+06 
               
               
                   
                 310 
                 4.946e+06 
               
               
                   
                   
               
            
           
         
       
     
     While preferred embodiments of the invention have been shown and described, modifications thereof can be made by one skilled in the art without departing from the spirit and teachings of the invention. The embodiments described herein are exemplary only, and are not intended to be limiting. Many variations and modifications of the invention disclosed herein are possible and are within the scope of the invention. Specifically, while the process is described in terms of a continuous process, it is contemplated that the process can be implemented as a batch process. In addition, where numerical ranges or limitations are expressly stated, such express ranges or limitations should be understood to include iterative ranges or limitations of like magnitude falling within the expressly stated ranges or limitations (e.g., from about 1 to about 10 includes, 2, 3, 4, etc.; greater than 0.10 includes 0.11, 0.12, 0.13, etc.). Use of the term “optionally” with respect to any element of a claim is intended to mean that the subject element is required, or alternatively, is not required. Both alternatives are intended to be within the scope of the claim. Use of broader terms such as comprises, includes, having, etc. should be understood to provide support for narrower terms such as consisting of, consisting essentially of, comprised substantially of, etc. Moreover, the percentages described herein may be mole fraction, weight fraction, or volumetric fraction. 
     Accordingly, the scope of protection is not limited by the description set out above but is only limited by the claims which follow, that scope including all equivalents of the subject matter of the claims. Each and every claim is incorporated into the specification as an embodiment of the present invention. Thus, the claims are a further description and are an addition to the preferred embodiments of the present invention. The discussion of a reference in the herein is not an admission that it is prior art to the present invention, especially any reference that may have a publication date after the priority date of this application. The disclosures of all patents, patent applications, and publications cited herein are hereby incorporated by reference, to the extent that they provide exemplary, procedural or other details supplementary to those set forth herein.