AU2016273827C1 - Single-unit gas separation process having expanded, post-separation vent stream - Google Patents

Abstract

\\davies.lcalmeldfs\redirected\kll\Desktop\Divisional pages - 35259298.doc-12//2016 A process comprising separating a hydrocarbon feed stream into a natural gas-rich stream and a liquefied petroleum gas (LPG)-rich stream using process equipment comprising only one multi-stage separation column, wherein the natural gas-rich stream has an energy content of less than or equal to about 1,300 British thermal units per cubic foot (Btu/ft), and wherein the LPG rich stream has a vapor pressure less than or equal to about 350 pounds per square inch gauge (psig). A process comprising separating a hydrocarbon feed stream into a top effluent stream and a LPG-rich stream, and subsequently expanding the top effluent stream to produce a natural gas-rich stream. An apparatus comprising a multi-stage separation column configured to separate a hydrocarbon feed stream into a top effluent stream and a LPG-rich stream, and an expander configured to expand the top effluent stream and produce a natural gas-rich stream.

Description

Single-Unit Gas Separation Process Having Expanded, Post-Separation Vent Stream CROSS-REFERENCE TO RELATED APPLICATIONS [0001] to [0003] Deleted.

BACKGROUND [0004] Typical gas processing options for high British thermal unit (Btu) gas (i.e. natural gas having a relatively high energy content) include cryogenic processing and refrigeration plants (e.g., a Joule-Thomson (JT) plant, a refrigerated JT plant, or a refrigeration only plant). Cryogenic processes generally comprise a refrigeration step to liquefy some or all of the gas stream followed by a multi-stage separation to remove methane from the liquid products. This process can capture very high (50-95%) ethane percentages, high propane percentages (9899%), and essentially all (e.g., 100%) of the heavier components. The residual gas from the process will typically have a Btu content meeting a natural gas pipeline specification (e.g. a Btu content of less than about 1,100 Btu/ft³). The liquid product from a cryogenic process can have a high vapor pressure that precludes the liquid from being a truckable product (e.g., a vapor pressure of greater than 250 pounds per square inch gauge (psig)). When a truckable product is required, the liquid product from the cryogenic plant will have to be “de-ethanized” prior to trucking by passing the liquid product through another separation step, and at least some of the ethane can be

2016273827 12 Dec 2016 blended back into the residual gas stream. Cryogenic processes face several constraints and limitations including high capital and operating costs, a high ethane recovery in the liquid product that may make the liquid unmarketable in certain areas, and the requirement for a pipeline to be located nearby.

(0005] Refrigeration plants are typically reserved for smaller volumes or stranded assets not near a pipeline. This process generally comprises cooling the inlet gas stream using the .IT effect and/or refrigeration followed by a single stage separation. These plants have a lower cost than cryogenic plants, but capture only 30-40% of propane, 80-90% of butanes, and close to 100% of the heavier components. Due to the reduced quantity of light components (e.g., methane and ethane), the liquid product is truckable. However, the lower propane recovery may result in the loss of potentially valuable product and a residual gas product with a high energy content, which can cause the residual gas to exceed the upper limit on the pipeline gas energy content. The reduced propane recovery can also prevent the residual gas from meeting the hydrocarbon dewpoint criteria as set by pipeline operators in certain markets. Additional propane can be recovered from refrigeration plants by increasing the refrigeration duty and/or the pressure drop through the plant, but because the process comprises a single stage, it also causes an increased ethane recovery, which raises the vapor pressure of the liquid product.

[0006] In many places, gas is produced that cannot be processed economically under either of the options presented above. The produced gas may have a range of compositions with an energy content ranging from about 1,050 to about 1,700 Btu/ fit³ or higher, and may have a nitrogen and/or contaminate (e.g., CO2, H2S, etc.) contents in excess of pipeline specifications. The gas may require a truckable liquid product due to the lack of a natural gas liquids (NGL) pipeline in the vicinity, and the residual gas product can require a high level of propane recovery

2016273827 12 Dec 2016 to meet the energy content specifications of a gas pipeline. Further, the gas may be produced in insufficient quantities to justify the expense of a cryogenic plant.

SUMMARY [0007] In one aspect, the disclosure includes a process comprising separating a hydrocarbon feed stream into a natural gas-rich stream and a liquefied petroleum gas (LPG)-rich stream using process equipment comprising only one multi-stage separation column, wherein the natural gasrich stream has an energy content of less than or equal to about 1,300 Btu/ft³, and wherein the LPG-rich stream has a vapor pressure less than or equal to about 350 psig.

[0008] In another aspect, the disclosure includes a process comprising separating a hydrocarbon feed stream into a top effluent stream and a LPG-rich stream, and subsequently expanding the top effluent stream to produce a natural gas-rich stream.

[0009] In another aspect, the disclosure includes an apparatus comprising a multi-stage separation column configured to separate a hydrocarbon feed stream into a natural gas-rich stream and a LPG-rich stream, wherein the natural gas-rich stream has an energy content of less than or equal to about 1,300 Btu/ft³, wherein the LPG-rich stream has a vapor pressure less than or equal to about 350 psig, and wherein the multi-stage separation column is the only multi-stage separation column in the apparatus.

[0010] In yet another aspect, the disclosure includes an apparatus comprising a multi-stage separation column configured to separate a hydrocarbon feed stream into a top effluent stream and a LPG-rich stream, and an expander configured to expand the top effluent stream and produce a natural gas-rich stream.

[0011] These and other features will be more clearly understood from the following detailed description taken in conjunction with the accompanying drawings and claims.

C:\Interwoven\NRPortbl\DCC\MDT\18619915_l.doc - 18/04/19

2016273827 18 Apr 2019 [0011a] According to one aspect, the present disclosure provides an apparatus comprising: a multi-stage separation column configured to separate a hydrocarbon feed stream into a top effluent stream and a liquefied petroleum gas (LPG)-rich stream; an expander configured to expand the top effluent stream and produce a natural gas-rich stream; a compressor configured to compress the natural gas-rich stream; a first heat exchanger configured to partially condense the top effluent stream into a vapor portion and a liquid portion; a reflux separator configured to separate the vapor portion from the liquid portion; a second heat exchanger configured to cool the hydrocarbon feed stream using the natural gas-rich stream; and a third heat exchanger configured to cool the hydrocarbon feed stream using mechanical refrigeration, wherein the liquid portion is returned to the multi-stage separation column as reflux, wherein the multistage separation column and the reflux separator are the only two separators in the apparatus, wherein the expander is a Joule-Thomson expander, and wherein the Joule-Thompson expander receives the vapor portion from the reflux separator and feeds an expanded natural gas-rich stream to the first heat exchanger.

[0011b] According to a further aspect, the present disclosure provides a method comprising: separating a hydrocarbon feed stream into a top effluent stream and a liquefied petroleum gas (LPG)-rich stream; expanding the top effluent stream to produce a natural gas-rich stream by receiving a vapor portion from a reflux separator at a Joule-Thompson expander and producing an expanded natural gas-rich stream with the Joule-Thompson expander; feeding the expanded natural gas-rich stream from the Joule-Thompson expander to a first heat exchanger; partially condensing the top effluent stream into the vapor portion and a liquid portion; separating the vapor portion from the liquid portion; cooling the hydrocarbon feed stream using the natural gas-rich stream; and cooling the hydrocarbon feed stream using mechanical refrigeration.

[0011c] According to a further aspect, the present disclosure provides a set of process equipment comprising: first piping configured to receive a hydrocarbon feed stream from a hydrocarbon formation; a multi-stage separation column coupled to the first piping and configured to separate the hydrocarbon feed stream into a top effluent stream and a liquefied petroleum gas (LPG)-rich stream; second piping configured to receive the top effluent stream from the multi-stage separation column; a first heat exchanger coupled to the second piping 3A

C:\Interwoven\NRPortbl\DCC\MDT\18619915_l.doc - 18/04/19

2016273827 18 Apr 2019 and configured to partially condense the top effluent stream into a vapor portion and a liquid portion; a reflux separator coupled to the first heat exchanger and configured to separate the vapor portion from the liquid portion, wherein the multi-stage separation column and the reflux separator are the only two separators in the set of process equipment; and a JouleThomson expander coupled to the reflux separator and configured to receive the vapor portion from the reflux separator, produce an expanded natural gas-rich stream, and feed the expanded natural gas-rich stream to the first heat exchanger.

3B

2016273827 12 Dec 2016

BRIEF DESCRIPTION OF THE DRAWINGS [0012] For a more complete understanding of this disclosure, reference is now made to the following brief description, taken in connection with the accompanying drawings and detailed description, wherein like reference numerals represent like parts.

[0013] FIG. I is a process flow diagram for an embodiment of a single-unit gas separation process having expanded, post-separation vent stream.

[0014] FIG. 2 is a schematic diagram of an embodiment of a single-unit gas separation process having expanded, post-separation vent stream.

[0015] FIG. 3 is a schematic diagram of another embodiment of a single-unit gas separation , process having expanded, post-separation vent stream.

i [0016] FIG. 4 is a schematic diagram of another embodiment of a single-unit gas separation process having expanded, post-separation vent stream.

[0017] FIG. 5 is a schematic diagram of another embodiment of a single-unit gas separation process having expanded, post-separation vent stream.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS |0018] It should be understood at the outset that although an illustrative implementation of ! one or more embodiments are provided below, the disclosed systems and/or methods may be

I ^! implemented using any number of techniques, whether currently known or in existence. The i

I disclosure should in no way be limited to the illustrative implementations, drawings, and | techniques illustrated below, including the exemplary designs and implementations illustrated i

and described herein, but may be modified within the scope of the appended claims along with i their full scope of equivalents.

:

2016273827 12 Dec 2016 [0019] Disclosed herein is a process and associated process equipment for a gas separation process that may use a single multi-stage column and a partial condensation of the column overhead to produce vapor and liquid portions. The liquid portion may be used as column reflu,x, while the vapor portion may be expanded and used to cool the column overhead and/or hydrocarbon feed stream. The present process provides a truckable NGL product along with a natural gas product that can be transported through a natural gas pipeline.

[0020| FIG. I illustrates a process flow diagram of a separation process 10. The gas separation process 10 may receive a hydrocarbon feed stream, which may undergo temperature and/or pressure adjustments 20. The temperature and/or pressure adjustments may include one or more heat exchangers and at least one mechanical refrigeration unit that cool the hydrocarbon fee stream. The heat exchangers may be cross exchangers with the cooled expanded stream from the expansion process 60. The temperature and/or pressure adjustments may reduce the amount of expansion required for the overhead stream to produce the reflux. The hydrocarbon Teed stream may then undergo a separation step 30, producing a top effluent stream and a bottom effluent stream. The separation step 30 may occur in the only multi-stage separator in the gas separation process 10. The top effluent stream may undergo a partial condensation step 40 to produce a mixed vapor and liquid stream. The exchanger may be a cross exchanger with the output from the overhead expansion process 60.

[0021] The mixed stream may undergo a separation step 50 to produce a liquid portion stream and a vapor portion stream. The liquid portion stream may be recycled to the separation process 30 as reflux. The vapor portion stream formed by the separation process 50 may be cooled by an expansion process 60 (e.g., using a JT expander or an expansion turbine). The expanded overhead stream may undergo further temperature and/or pressure adjustments 70 to create a natural gas-rich stream suitable for entry into a pipeline. Temperature and/or pressure adjustment 70 may comprise any known hydrocarbon temperature and/or pressure adjustment process. For example, the overhead stream may be heated, cooled, compressed, throttled, expanded or combinations thereof. The overhead stream may be cross-exchanged with other streams in the single-unit gas separation process 10 to exchange heat between the streams.

[0022] FIG. 2 illustrates one embodiment of a gas separation process 100. The gas separation process 100 separates the hydrocarbon feed stream 201 into a LPG-rich stream 206 and a natural gas-rich stream 219, which may be suitable for a gas pipeline. The process 100 receives the hydrocarbon feed stream 201 and may pass the hydrocarbon feed stream 201 through a heat exchanger 101 that uses the overhead stream 214 to reduce the temperature of the hydrocarbon feed stream 201. The cooled feed stream 202 may then pass through a mechanical refrigeration unit 102, which may give off energy 301 to refrigerate the cooled feed stream 202, and produce a refrigerated feed stream 203. The refrigerated feed stream 203 may then be passed to a multi-stage separator column 104, which separates the refrigerated feed stream 203 into a bottom effluent stream 205 and a top effluent stream 208. The bottom effluent stream 205 may be fed into a reboiler 105, which may receive energy 302 by being heated, and which separates the bottom effluent stream 205 into a boil-up stream 207 and the LPG-rich stream 206. The top effluent stream 208 may pass through a heat exchanger 106 cross-exchanged with the expanded overhead stream 213 to at least partially condense the top effluent stream 208, thereby producing a mixed stream 209 comprising liquid and vapor portions. The mixed stream 209 may be fed into the separator 107 that separates the liquid portion stream 210 from the vapor portion stream 212. The liquid portion stream 210 may be passed through pump 108 to control the rate at which reflux stream 211 is fed back into the multi-stage separator column 104.

2016273827 12 Dec 2016 [0023] Returning to the separator 107, the vapor portion stream 212 may be fed into an expander 113, specifically a JT expander, to reduce the temperature and/or pressure of the vapor portion stream 212. The expanded overhead stream 213 may pass through the heat exchanger 106 to increase the temperature of the expanded overhead stream 213 and/or to decrease the temperature of top effluent stream 208. The overhead stream 214 may then be passed through the heat exchanger 101 to further increase the temperature of the overhead stream 214 and/or to cool the hydrocarbon feed stream 201. The residue stream 216 may be passed through a compressor 110 receiving energy 305 to increase the pressure and/or temperature in the residue stream 216 creating the pressurized residue stream 217. The pressurized residue stream 217 may be passed through a heat exchanger 111 to cool the pressurized residue stream 217 creating the cooled pressurized residue stream 218. The cooled pressurized residue stream 218 may be passed through a compressor 112 receiving energy 304 to increase the pressure and/or temperature in the cooled pressurized residue stream 218 to create a natural gas-rich stream 219.

[0024] FIG. 3 illustrates an embodiment of a gas separation process 150. As in the gas separation process 100 described above, the gas separation process 150 separates the hydrocarbon feed stream 201 into a LPG-rich stream 206 and a natural gas-rich stream 219. The gas separation process 150 receives the hydrocarbon feed stream 201 and may pass the hydrocarbon feed stream 201 through a heat exchanger 101 that uses a warmed residue stream 215 to reduce the temperature of the hydrocarbon feed stream 201, and produce a cooled feed stream 202. The cooled feed stream 202 may then pass through a mechanical refrigeration unit 102, which may give off energy 301 to refrigerate the cooled feed stream 202. The refrigerated feed stream 203 may be passed through a heat exchanger 103 that uses the overhead stream 214 to reduce the temperature of the refrigerated feed stream 203, and produce a chilled feed stream

2016273827 12 Dec 2016

204. The remaining streams and process equipment in the gas separation process 150 are substantially the same as the corresponding streams and process equipment in the gas separation process 100.

[0025] FIG. 4 illustrates an embodiment of a gas separation process 160. In the gas separation process 160, the hydrocarbon feed stream 201 may be processed similar to the hydrocarbon feed stream 201 in the gas separation process 100 to create a LPG-rich stream 206 and a vapor portion stream 212. The vapor portion stream 212 may be passed through an expander 109, specifically an expansion turbine, which reduces the temperature and/or pressure of vapor portion stream 212 and produces energy 303 (e.g. mechanical or electrical energy). The expander 109 may be coupled to a compressor 110 such that the energy stream 303 created by the expansion process is used to run the compressor 110. The remaining streams and process equipment in the gas separation process 160 are substantially the same as the corresponding streams and process equipment in the gas separation process 100.

[0026] FIG. 5 illustrates an embodiment of a gas separation process 170. In the gas separation process 170, the hydrocarbon feed stream 201 may be processed similar to the hydrocarbon feed stream 201 in the gas separation process 150 to produce the LPG-rich stream 206 and a vapor portion stream 212. However, the vapor portion stream 212 may be processed similar to the vapor portion stream 212 in the gas separation process 160 to create a natural-gas rich stream 219. The remaining streams and process equipment in the gas separation process 170 are substantially the same as the corresponding streams and process equipment in the gas separation process 150.

[0027] The hydrocarbon feed stream may contain a mixture of hydrocarbons and other compounds. Numerous types of hydrocarbons may be present in the hydrocarbon feed stream,

2016273827 12 Dec 2016 including methane, ethane, propane, i-butane, n-butane, i-pentane, n-pentane, hexane, heptane, octane, and other hydrocarbons. Other compounds may be present in the hydrocarbon feed stream, including nitrogen, carbon dioxide, water, helium, hydrogen sulfide, other acid gases, and/or impurities. The hydrocarbon feed stream may be in any state including a liquid state, a vapor state, or a combination of liquid and vapor states. In an embodiment, the hydrocarbon feed stream may be substantially similar in composition to the hydrocarbons in the subterranean formation, e.g. the hydrocarbons may not be processed prior to entering the gas separation process described herein. Alternatively, the hydrocarbon feed stream may be sweetened, but is not otherwise refined or separated.

[0028] The composition of the hydrocarbon feed stream may differ from location to location. In embodiments, the hydrocarbon feed stream comprises from about 45 percent to about 99 percent, from about 60 percent to about 90 percent, or from about 70 percent to about 80 percent methane. Additionally or alternatively, the hydrocarbon feed stream may comprise from about I percent to about 25 percent, from about 2 percent to about 18 percent, or from about 4 percent to about 12 percent ethane. Additionally or alternatively, the hydrocarbon feed stream may comprise from about I percent to about 25 percent, from about 2 percent to about 20 percent, or from about 3 percent to about 9 percent propane. In embodiments, the hydrocarbon feed stream may have an energy content of less than or equal to about 2,000 Btu/ft³, from about 900 Btu/ft³ to about 1,800 Btu/ft³, or from about 1,100 Btu/ft³ to about 1,600 Btu/ft³. Unless otherwise stated, the percentages herein are provided on a mole basis.

[0029] The LPG-rich stream may contain a mixture of hydrocarbons and other compounds. Numerous types of hydrocarbons may be present in the LPG-rich stream, including methane, ethane, propane, i-butane, n-butane, i-pentane, n-pentane, hexane, heptane, octane, and other

2016273827 12 Dec 2016 hydrocarbons. Other compounds may be present in the LPG-rich stream, including nitrogen, carbon dioxide, water, helium, hydrogen sulfide, other acid gases, and/or other impurities. Specifically, the LPG-rich stream comprises less than or equal to about 6 percent, less than or equal to about 4 percent, less than or equal to about 2 percent, or is substantially free of methane. Additionally or alternatively, the LPG-rich stream may comprise from about 8 percent to about 35 percent, from about 10 percent to about 28 percent, or from about 15 percent to about 25 percent ethane. Additionally or alternatively, the LPG-rich stream may comprise from about 10 percent to about 60 percent, from about 20 percent to about 50 percent, or from about 24 percent to about 33 percent propane. In embodiments, the LPG-rich stream may have a vapor pressure less than or equal to about 600 psig, less than or equal to about 250 psig, or less than or equal to about 200 psig, which may be determined according to ASTM-D-323.

[0030| In embodiments, the LPG-rich stream may contain an increased propane concentration and a decreased methane concentration compared to the hydrocarbon feed stream. In embodiments, the LPG-rich stream may comprise less than or equal to about 15 percent, less than or equal to about 7 percent, or less than or equal to about 3 percent of the methane in the hydrocarbon feed stream. Additionally or alternatively, the LPG-rich stream may comprise from about 10 percent to about 55 percent, from about 20 percent to about 53 percent, or from about 40 percent to about 50 percent of the ethane in the hydrocarbon feed stream. Additionally or alternatively, the LPG-rich stream may comprise greater than or equal to about 40 percent, greater than or equal to about 60 percent, or greater than or equal to about 85 percent of the propane in the hydrocarbon feed stream.

[0031] The natural gas-rich stream may contain a mixture of hydrocarbons and other compounds. Numerous types of hydrocarbons may be present in the natural gas-rich stream,

2016273827 12 Dec 2016 including methane, ethane, propane, i-butane, n-butane, i-pentane, n-pentane, hexane, heptane, octane, and other hydrocarbons. Other compounds may be present in the natural gas-rich stream, including nitrogen, carbon dioxide, water, helium, hydrogen sulfide, other acid gases, and/or other impurities. Specifically, the natural gas-rich stream comprises greater than or equal to about 65 percent, from about 75 percent to about 99 percent, or from about 85 percent to about 95 percent methane. Additionally or alternatively, the natural gas-rich stream may comprise less than about 30 percent, from about I percent to about 20 percent, or from about 2 percent to about 8 percent ethane. Additionally or alternatively, the natural gas-rich stream may be less than about 1 percent or be substantially free of propane. In embodiments, the natural gas-rich stream may have an energy content of less than or equal to about 1,300 Btu/ft³, from about 900 Btu/fr⁵ to about 1,200 Btu/ft³, from about 950 Btu/ft³ to about 1,150 Btu/ft³, or from about 1,000 Btu/ft³ to about 1,100 Btu/ft³.

[0032| In embodiments, the natural gas-rich stream may contain an increased methane concentration and a decreased propane concentration compared to the hydrocarbon feed stream 201. In embodiments, the natural gas-rich stream may contain greater than or equal to about 85 percent, greater than or equal to about 93 percent, or greater than or equal to about 97 percent of the methane in the hydrocarbon feed stream. Additionally or alternatively, the natural gas-rich stream may comprise from about 45 percent to about 90 percent, from about 47 percent to about 80 percent, or from about 50 percent to about 60 percent of the ethane in the hydrocarbon feed stream. Additionally or alternatively, the natural gas-rich stream may comprise less than or equal to about 60 percent, less than or equal to about 40 percent, or less than or equal to about 15 percent of the propane in the hydrocarbon feed stream.

2016273827 12 Dec 2016 [0033] The separators described herein 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. At least one of the separators may be a multi-stage separation column, in which the separation process occurs at multiple stages having unique temperature and pressure gradients. A multi-stage separation column 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. Additionally or alternatively, one or more of the separators may be a single stage separation column such as a phase separator. A phase separator is a vessel that separates an inlet stream into a substantially vapor stream and a substantially liquid stream without a substantial change between the state of the feed entering the vessel and the state of the fluids inside the vessel. 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. For example, the phase separator may be a knockout drum or a flash drum. Finally, one or more of the separators may be any other type of separator, such as a membrane separator.

[0034] The expanders described herein may be any of a variety of process equipment capable of cooling a gas stream. For example, the expanders may be a JT expander, e.g. any device that cools a stream primarily using the JT effect, such as throttling devices, throttling valves, or a porous plug. Alternatively, the expanders may be expansion turbines. Generally, expansion

2016273827 12 Dec 2016 turbines, also called turboexpanders, include a centrifugal or axial flow turbine connected to a drive a compressor or an electric generator. The types of expansion turbines suitable include turboexpanders, centrifugal or axial flow turbines.

[0035] The heat exchangers 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 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 suitable for the gas separation process include shell and tube, kettle-type, air-cooled, bayonet, plate-fin, and spiral heat exchangers.

[0036] The mechanical refrigeration unit described herein may be any of a variety of process equipment comprising a suitable refrigeration process. The refrigeration fluid that circulates in the mechanical refrigeration unit may be any suitable refrigeration fluid, such as methane, ethane, propane, FREON, or combinations thereof.

[0037] The reboiler 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 reboiler 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 described herein.

[0038] The compressors 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

2016273827 12 Dec 2016 herein. Generally, compressors are associated with vapor streams; however, such a limitation should not be read into the present processes as the compressors described herein may be interchangeable with pumps 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 gas separation processes described herein may contain additional compressors and/or pumps other than those described herein.

[0039] The pump 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. The types of pumps suitable for the uses described herein include centrifugal, axial, positive displacement, rotary, and reciprocating pumps. Finally, the gas separation processes described herein may contain additional pumps other than those described herein.

[0040] The energy streams 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. In addition, persons of ordinary skill in the art will appreciate that the gas separation processes

2016273827 12 Dec 2016 described herein may contain additional equipment, process streams, and/or energy streams other than those described herein.

[0041] The gas separation process having an expanded, post-separation vent stream described herein has many advantages. One advantage is the use of only one multi-stage separator column. This is an advantage because it reduces the capital costs of building and operating the process. A second advantage is the process produces both a truckable LPG-rich stream and a pipeline suitable natural gas-rich stream. When combined with heat integration, the process may be able to recover a high percentage (e.g., about 85 to about 98%) of the propane in the LPG-rich stream while rejecting enough ethane to make a truckable product (e.g., a vapor pressure less than about 350 psig) as well as meet pipeline specifications on the natural gas-rich stream (e.g., a heat content of less than about 1,100 Btu/ft³, a dew point specification, etc.).

EXAMPLES [0042] In one example, a process simulation was performed using the single-unit gas separation process 100 shown in FIG. 2. The simulation was performed using the Aspen HYSYS Version 7.2 software package. The material streams, their compositions, and the associated energy streams produced by the simulation are provided in Tables 1-3 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 (Ib/hr), barrels per day (barrel/day), Btu/ft³, and Btu/hr.

Property	201	202	203	206	208
Vapor Fraction	0.9365	0.8579	0.7091	0.0005	1
Temperature	(F)	100*	50.79	-20	253.1	-48.66
Pressure	(psig)	800*	795	790	705	700
Molar Flow	(MMSCFD)	25*	25	25	4.739	23.97
Mass Flow	(Ib/hr)	65540	65540	65540	26920	47600
Liquid Vol. Flow (barrel/day)	11850	11850	11850	3457	10150
Heat Flow	(Btu/hr)	-1.01E+08	-1.04E+08	-1.08E+08	-2.72E+07	-9.17E+07

Table IA: FIG. 2 Single-Unit Gas Separator Stream Properties

Property	209	210	211	212	213
Vapor Fraction	0.8466	0	0	1	0.9473
Temperature	(F)	-80.76	-80.59	-78.76	-80.59	-136.7
Pressure	(psig)	695	695	795	695	200
Molar Flow	(MMSCFD)	23.97	3.705	3.705	20.17	20.17
Mass Flow	(Ib/hr)	47600	8980	8980	38480	38480
Liquid Vol. Flow (barrel/day)	10150	1757	1757	8359	8359
Heat Flow	(Btu/hr)	-9.38E+07	-1.64E+07	-1.64E+07	-7.71E+07	-7.71 E+07

Table IB: FIG. 2 Single-Unit Gas Separator Stream Properties

Property	214	216	217	218	219
Vapor Fraction	1	1	1	1	1
Temperature	(F)	-60	80	150.2	120	293 7
Pressure	(psig)	195	192	300	295	800
Molar Flow	(MMSCFD)	20.17	20.17	20.17	20.17	21.17
Mass Flow	(Ib/hr)	38480	38480	38480	38480	38480
Liquid Vol. Flow (barrel/day)	8359	8359	8359	8359	8359
Heat Flow	(Btu/hr)	-7.49E+07	-7.21 E+07	-7.07E+07	-7.14E+07	-6.79E+07

Table 1C: FIG. 2 Single-Unit Gas Separator Stream Properties

	201	206	219
Energy Content (Btu/ft3)	1395.72		1043.91
Vapor Pressure (psig)		250

Table ID: FIG. 2 Single-Unit Gas Separator Stream Properties

Mole Frac	201	202	203	206	208	209	210	211
Nitrogen	0.0162*	0.0162	0.0162	0.0000	0.0178	0.0178	0.0059	0.0059
CO2	0.0041*	0.0041	0.0041	0.0040	0.0047	0.0047	0.0075	0.0075
Methane	0.7465*	0.7465	0.7465	0.0220	0.8807	0.8807	0.6878	06878
Ethane	0.0822*	0.0822	0.0822	0.2120	0.0739	0.0739	0.1944	0.1944
Propane	0.0608*	0.0608	0.0608	0.2881	0.0216	0.0216	0.0980	0.0980
i-Butane	0.0187*	0.0187	0.0187	0.0972	0.0008	0.0008	0.0035	0.0035
n-Butane	0.0281*	0.0281	0.0281	0.1477	0.0005	0.0005	0.0026	0 0026
i-Pentane	0.015*	0.0150	0.0150	0.0791	0.0000	0.0000	0.0002	0.0002
n-Pentane	0.0169*	0.0169	0.0169	0.0892	0.0000	0.0000	0.0001	0.0001
Hexane	0.006*	0.0060	0.0060	0.0317	0.0000	0.0000	0.0000	0.0000
Heptane	0.004*	0.0040	0.0040	0.0211	0.0000	0.0000	0.0000	0.0000
Octane	0.0015*	0.0015	0.0015	0.0079	0.0000	0.0000	0.0000	0.0000
Water	0*	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
H2S	0*	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000

Table 2A: FIG. 2 Single-Unit Gas Separator Stream Compositions

2016273827 12 Dec 2016

Mole Frac	212	213	214	216	217	218	219
Nitrogen	0.0200	0.0200	0.0200	0.0200	0.0200	0.0200	0.0200
CO2	0.0041	0.0041	0.0041	0.0041	0.0041	0.0041	0.0041
Methane	0.9152	0.9152	0.9152	0.9152	0.9152	0.9152	0.9152
Ethane	0.0521	0.0521	0.0521	0.0521	0.0521	0.0521	0.0521
Propane	0.0084	0.0084	0.0084	0.0084	0.0084	0.0084	0.0084
i-Butane	0.0001	0.0001	0.0001	0.0001	0.0001	0.0001	0.0001
n-Butane	0.0001	0.0001	0.0001	0.0001	0.0001	0.0001	0.0001
i-Pentane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
n-Pentane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Hexane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Heptane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Octane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Water	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
H2S	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000

Table 2B: FIG. 2 Single-Unit Gas Separator Stream Compositions

Energy Flow	301	302	304	305	306
Btu/hr	4,119,000	5,822,000	3,526,000	1,349,000	9,863

Table 3: FIG. 2 Single-Unit Gas Separator Energy Streams [0043] A second process simulation was performed using the single-unit gas separation process 100 shown in FIG. 2. The simulation was performed using the Aspen HYSYS Version

7.2 software package. This second simulation was run with a different feed composition. The material streams, their compositions, and the associated energy streams produced by the simulation are provided in Tables 4-6 below. The specified values are indicated by an asterisk (*). The physical properties are provided in degrees F, psig, MMSCFD, Ib/hr, barrel/day.

Btu/ft³, and Btu/hr.

Property	201	202	203	206	208
Vapor Fraction	0.9219	0.8576	0 5038	0	1
Temperature	(F)	100*	82.57	-20	168.6	-8.961
Pressure	(psig)	400*	395	390	405	400
Molar Flow	(MMSCFD)	1*	1	1	0.3496	0.6786
Mass Flow	(Ib/hr)	3299	3299	3299	1845	1564
Liquid Vol. Flow (barrel/day)	531.6	531.6	531.6	245.4	303.1
Heat Flow	(Btu/hr)	-4.372E+06	-4.440E+06	-4.811E+06	-2.021 E+06	-2.649E+06

Table 4A: FIG. 2 Single-Unit Gas Separator Stream Properties

2016273827 12 Dec 2016

Property	209	210	211	212	213
Vapor Fraction	0.9584	0	0	1	1
Temperature	(F)	-24.54	-24.51	-23.4	-24.51	-61.48
Pressure	(psig)	395	395	495	395	100
Molar Flow	(MMSCFD)	0.6786	0.02819	0.002819	0.6502	0.6502
Mass Flow	(lb/hr)	1564	110	110	1454	1454
Liquid Vol. Flow (barrel/day)	303.1	17.02	17.02	286.1	286.1
Heat Flow	(Btu/hr)	-2.677E+06	-1.540E+05	-1.539E+05	-2.52E+06	-2.52E+06

Table 4B: FIG. 2 Single-Unit Gas Separator Stream Properties

Property	214	216	217	218	219
Vapor Fraction	1	1	1	1	1
Temperature	(F)	-20	80	251.3	120	232.3
Pressure	(psig)	95	92	300	295	600
Molar Flow	(MMSCFD)	0.6502	0.6502	0.6502	0.6502	0.6502
Mass Flow	(lb/hr)	1454	1454	1454	1454	1454
Liquid Vol. Flow (barrel/day)	286.1	286.1	286.1	286.1	286.1
Heat Flow	(Btu/hr)	-2.49E+06	-2.43E+06	-2.31 E+06	-2.41E+06	-2.33E+06

Table 4C: FIG. 2 Single-Unit Gas Separator Stream Properties

	201	206	219
Energy Content (Btu/ft3)	1682.1		1123.9
Vapor Pressure (psig)		200

Table 4D: FIG. 2 Single-Unit Gas Separator Stream Properties

Mole Frac	201	202	203	206	208	209	210	211
Nitrogen	0.032*	0.0320	0.0320	0.0000	0.0473	0.0473	0.0039	0.0039
CO2	0.0102*	0.0102	0.0102	0.0008	0.0151	0.0151	0.0118	0.0118
Methane	0.4896*	0.4896	0.4896	0.0009	0.7296	0.7296	0.2056	0.2056
Ethane	0.1486*	0.1486	0.1486	0.1743	0.1412	0.1412	0.2871	0.2871
Propane	0.1954*	0.1954	0.1954	0.4762	0.0593	0.0593	0.3995	0.3995
i-Butane	0.0692*	0.0692	0.0692	0.1916	0.0065	0.0065	0.0778	0.0778
n-Butane	0.0285*	0.0285	0.0285	0.0806	0.0011	0.0011	0.0140	0.0140
i-Pentane	0.0102*	0.0102	0.0102	0.0291	0.0000	0.0000	0.0001	0.0001
n-Pentane	0.0102*	0.0102	0.0102	0.0291	0.0000	0.0000	0.0001	0.0001
Hexane	0.002*	0.0020	0.0020	0.0058	0.0000	0.0000	0.0000	0.0000
Heptane	0.002*	0.0020	0.0020	0.0058	0.0000	0.0000	0.0000	0.0000
Octane	0.002*	0.0020	0.0020	0.0058	0.0000	0.0000	0.0000	0.0000
Water	0*	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
H2S	0*	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000

Table 5A: FIG. 2 Single-Unit Gas Separator Stream Properties

2016273827 12 Dec 2016

Mole Frac	212	213	214	216	217	218	219
Nitrogen	0.0491	0.0491	0.0491	0.0491	0.0491	0.0491	0.0491
CO2	0.0152	0.0152	0.0152	0.0152	0.0152	0.0152	0.0152
Methane	0.7515	0.7515	0.7515	0.7515	0.7515	0.7515	0.7515
Ethane	0.1355	0.1355	0.1355	0.1355	0.1355	0.1355	0.1355
Propane	0.0451	0.0451	0.0451	0.0451	0.0451	0.0451	0.0451
i-Butane	0.0032	0.0032	0.0032	0.0032	0.0032	0.0032	0.0032
n-Butane	0.0004	0.0004	0.0004	0.0004	0.0004	0.0004	0.0004
i-Pentane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
n-Pentane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Hexane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Heptane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Octane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Water	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
H2S	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000

Table 5B: FIG. 2 Single-Unit Gas Separator Stream Properties

Energy Flow	301	302	304	305	306
Btu/hr	370,100	295,000	76,450	120,400	86

Tab e 6: FIG. 2 Single-Unit Gas Separator Stream Properties [0044] In another example, a process simulation was performed using the single-unit gas separation process 150 shown in FIG. 3. The simulation was performed using the Aspen

HYSYS Version 7.2 software package. The material streams, their compositions, and the associated energy streams produced by the simulation are provided in Tables 7-9 below. The specified values are indicated by an asterisk (*). The physical properties are provided in degrees

F, psig, MMSCFD, Btu/ft³, and Btu/hr.

Property	201	202	203	204	206	208
Vapor Fraction	0.9347	0.8577	0.7151	0.7109	0	1
Temperature	(F)	100*	52.44	-15	-17	256.3	-43.21
Pressure	(psig)	800*	795	790	785	710	700
Molar Flow	(MMSCFD)	25*	25	25	25	4.649	23.59
Mass Flow	(Ib/hr)	65540	65540	65540	65540	26550	47110
Liquid Vol. Flow (barrel/day)	11850	11850	11850	11850	3397	10010
Heat Flow	(Btu/hr)	-1.01E+08	-1.04E+08	-1.08E+08	-1.08E+08	-2.67E+07	-9.02E+07

Table 7A: FIG. 3 Single-Unit Gas Separator Stream Properties

Property	209	210	211	212	213	214
Vapor Fraction	0.8632	0	0	1	0.9532	1
Temperature	(F)	-76.43	-76.56	-74.79	-76.56	-132	-58
Pressure	(psig)	695	695	795	695	200	195
Molar Flow	(MMSCFD)	23.59	3.237	3.237	20.36	20.36	20.36
Mass Flow	(Ib/hr)	47110	8118	8118	38990	38990	38990
Liquid Vol. Flow (barrel/day)	10010	1559	1559	8453	8453	8453
Heat Flow	(Btu/hr)	-9.22E+07	-1.45E+07	-1.45E+07	-7.77E+07	-7.77E+07	-7.57E+07

Table 7B: FIG. 3 Single-Unit Gas Separator Stream Properties

Property	215	216	217	218	219
Vapor Fraction	1	1	1	1	1
Temperature	(F)	-53.46	80	222.2	120	221
Pressure	(psig)	190	187	450	445	800
Molar Flow	(MMSCFD)	20.36	20.36	20.36	20.36	20.36
Mass Flow	(Ib/hr)	38990	38990	38990	38990	38990
Liquid Vol. Flow (barrel/day)	8453	8453	8453	8453	8453
Heat Flow	(Btu/hr)	-7.55E+07	-7.28E+07	-7.00E+07	7.23E+07	-7.03E+07

Table 7C: FIG. 3 Single-Unit Gas Separator Stream Properties

	201	206	219
Energy Content (Btu/ft3)	1395.7		1042.3
Vapor Pressure (psig)		250

Table 7D: FIG. 3 Single-Unit Gas Separator Stream Properties

Mole Frac	201	202	203	204	206	208	209	210	211
Nitrogen	0.0162*	0.0162	0.0162	0.0162	0.0000	0.0179	0.0179	0.0054	0.0054
CO2	0.0041*	0.0041	0.0041	0.0041	0.0038	0.0046	0.0046	0.0074	0.0074
Methane	0.7465*	0.7465	0.7465	0.7465	0.0244	0.8772	0.8772	0.6618	0.6618
Ethane	0.0822*	0.0822	0.0822	0.0822	0.2036	0.0743	0.0743	0.1990	0.1990
Propane	0.0608*	0.0608	0.0608	0.0608	0.28501	0.0238	0.0238	0.1133	0.1133
i-Butane	0.0187	0.0187	0.0187	0.0187	0.0994	0.0013	0.0013	0.0081	0.0081
n-Butane	0.0281	0.0281	0.0281	0.0281	0.1505	0.0008	0.0008	0.0047	0.0047
i-Pentane	0.0150	0.0150	0.0150	0.0150	0.0806	0.0000	0.0000	0.0002	0.0002
n-Pentane	0.0169	0.0169	0.0169	0.0169	0.0909	0.0000	0.0000	0.0001	0.0001
Hexane	0.0060	0.0060	0.0060	0.0060	0.0323	0.0000	0.0000	0.0000	0.0000
Heptane	0.0040	0.0040	0.0040	0.0040	0.0215	0.0000	0.0000	0.0000	0.0000
Octane	0.0015	0.0015	0.0015	0.0015	0.0081	0.0000	0.0000	0 0000	0.0000
Water	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0 0000	0.0000
H2S	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000

able 8A: FIG. 3 Single-Unit Gas Separator Stream Compositions

Mole Frac	212	213	214	215	216	217	218	219
Nitrogen	0.0199	0.0199	0.0199	0.0199	0.0199	0.0199	0.0199	0.0199
CO2	0.0041	0.0041	0.0041	0.0041	0.0041	0.0041	0.0041	0.0041
Methane	0.9117	0.9117	0.9117	0.9117	0.9117	0.9117	0.9117	0.9117
Ethane	0.0544	0.0544	0.0544	0.0544	0.0544	0.0544	0.0544	0.0544
Propane	0.0095	0.0095	0.0095	0.0095	0.0095	0.0095	0.0095	0.0095
i-Butane	0.0003	0.0003	0.0003	0.0003	0.0003	0.0003	0.0003	0.0003
n-Butane	0.0001	0.0001	0.0001	0.0001	0.0001	0.0001	0.0001	0.0001
i-Pentane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
n-Pentane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Hexane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Heptane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Octane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Water	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
H2S	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000

Table 8B: FIG. 3 Single-Unit Gas Separator Stream Compositions

Energy Flow	301	302	304	305	306
Btu/hr	3,897,000	5,690,000	1,977,000	2,830,000	8,645

Table 9: FIG. 3 Single-Unit Gas Separator Energy Streams [0045] A second process simulation was performed using the single-unit gas separation process 150 shown in FIG. 3. The simulation was performed using the Aspen HYSYS Version

7.2 software package. This second simulation was run with a different feed composition. 1 he material streams, their compositions, and the associated energy streams produced by the simulation are provided in Tables 10-12 below. The specified values are indicated by an asterisk (*). The physical properties are provided in degrees F, psig, MMSCFD, Ib/hr, barrel/day,

Btu/ft³, and Btu/hr.

Property	201	202	203	204	206	208
Vapor Fraction	1	0.9608	0.7875	0.7796	0	1
Temperature	(F)	100*	40.14	-15	-17	227.7	-15.22
Pressure	(psig)	800*	795	790	785	710	700
Molar Flow	(MMSCFD)	25*	25	25	25	2.315	25.56
Mass Flow	(Ib/hr)	59670	59670	59670	59670	11930	56010
Liquid Vol. Flow (barrel/day)	11600	11600	11600	11600	1608	11510
Heat Flow	(Btu/hr)	-9.54E+07	-9.81 E+07	-1.02E+08	-1.02E+08	-1.23E+07	-9.85E+07

Table 10A: FIG. 3 Single-Unit Gas Separator Stream Properties

2016273827 12 Dec 2016

Property	209	210	211	212	213	214
Vapor Fraction	0.8884	0	0	1	0.9591	1
Temperature	(F)	-34.39	-34.49	-32.7	-34.49	-71.3	-30
Pressure	(psig)	695	695	795	695	300	295
Molar Flow	(MMSCFD)	25.56	2.878	2.878	22.7	22.7	22.7
Mass Flow	(Ib/hr)	56010	8273	8273	47760	47760	47760
Liquid Vol. Flow (barrel/day)	11510	1523	1523	9997	9997	9997
Heat Flow	(Btu/hr)	-1.00E+08	-1.31E+07	-1.31E+07	-8.70E+07	-8.70E+07	-8.55E+07

Table 1 OB: FIG. 3 Single-Unit Gas Separator Stream Properties

Property	215	216	217	218	219
Vapor Fraction	1	1	1	1	1
Temperature	(F)	-25.81	80	148.6	120	167.9
Pressure	(psig)	290	287	450	445	600
Molar Flow	(MMSCFD)	22.7	22.7	22.7	22.7	22.7
Mass Flow	(Ib/hr)	47760	47760	47760	47760	47760
Liquid Vol. Flow (barrel/day)	9997	9997	9997	9997	9997
Heat Flow	(Btu/hr)	-8.53E+07	-8.27E+07	-8.12E+07	-8.19E+07	-8.09E+07

Table 10C: FIG. 3 Single-Unit Gas Separator Stream Properties

	201	206	219
Energy Content (Btu/ft3)	1299.9		1132.9
Vapor Pressure (psig)		200

Table 10D: FIG. 3 Single-Unit Gas Separator Stream Properties

Mole Frac	201	202	203	204	206	208	209	210	211
Nitrogen	0.0158*	0.0158	0.0158	0.0158	0.0000	0.0159	0.0159	0.0038	0.0038
CO2	0.004*	0.0040	0.0040	0.0040	0.0004	0.0045	0.0045	0.0053	0.0053
Methane	0.7266*	0.7266	0.7266	0.7266	0.0042	0.7601	0.7601	0.4429	0.4429
Ethane	0.1616*	0.1616	0.1616	0.1616	0.2434	0.1793	0.1793	0.3851	0.3851
Propane	0.0592*	0.0592	0.0592	0.0592	0.4579	0.0323	0.0323	0.1410	0.1410
i-Butane	0.0059*	0.0059	0.0059	0.0059	0.0607	0.0007	0.0007	0.0043	0.0043
n-Butane	0.0111*	0.0111	0.0111	0.0111	0.1183	0.0005	0.0005	0.0034	0.0034
i-Pentane	0.0025*	0.0025	0.0025	0.0025	0.0270	0.0000	0 0000	0 0001	0.0001
n-Pentane	0.0034*	0.0034	0.0034	0.0034	0.0367	0.0000	0.0000	0.0000	0.0000
Hexane	0.0018*	0.0018	0.0018	0.0018	0.0194	0.0000	0.0000	0.0000	0.0000
Heptane	0.0001*	0.0010	0.0010	0.0010	0.0108	0.0000	0.0000	0.0000	0.0000
Octane	0.0001*	0.0010	0.0010	. 0.0010	0.0108	0.0000	0.0000	0.0000	0.0000
Water	0*	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
H2S	0.0062*	0.0062	0.0062	0.0062	0.0103	0.0067	0.0067	0.0142	0.0142

Table 11A: FIG. 3 Single-Unit Gas Separator Stream Compositions

2016273827 12 Dec 2016

Mole Frac	212	213	214	215	216	217	218	219
Nitrogen	0.0174	0.0174	0.0174	0.0174	0.0174	0.0174	0.0174	0 0174
CO2	0.0044	0.0044	0.0044	0.0044	0.0044	0.0044	0.0044	0 0044
Methane	0.8002	0.8002	0.8002	0.8002	0.8002	0.8002	0.8002	0.8002
Ethane	0.1534	0.1534	0.1534	0.1534	0.1534	0.1534	0.1534	0 1534
Propane	0.0185	0.0185	0.0185	0.0185	0.0185	0.0185	0.0185	0 0185
i-Butane	0.0003	0.0003	0.0003	0.0003	0.0003	0.0003	0.0003	0.0003
n-Butane	0.0002	0.0002	0.0002	0.0002	0.0002	0.0002	0.0002	0.0002
i-Pentane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
n-Pentane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Hexane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Heptane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Octane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Water	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
H2S	0.0058	0.0058	0.0058	0.0058	0.0058	0.0058	0.0058	0.0058

Table 1 IB: FIG. 3 Single-Unit Gas Separator Stream Compositions

Energy Flow	301	302	304	305	306
Btu/hr	3,470,000	3,949,000	1,063,000	1,511,000	8,293

Table 12: FIG. 3 Single-Unit Gas Separator Energy Streams [0046] In another example, a process simulation was performed using the single-unit gas separation process 160 shown in FIG. 4. The simulation was performed using the Aspen

I

I HYSYS Version 7.2 software package. The material streams, their compositions, and the associated energy streams produced by the simulation are provided in Tables 13-15 below. The specified values are indicated by an asterisk (*). The physical properties are provided in degrees F, psig, MMSCFD, Btu/ft³, and Btu/hr.

Property	201	202	203	206	208
Vapor Fraction	0.9352	0.8511	0.7101	0.0008	1
Temperature	(F)	100*	46.69	-20	249.9	-53.62
Pressure	(psig)	800*	795	790	705	700
Molar Flow	(MMSCFD)	25*	25	25	4.803	25.06
Mass Flow	(Ib/hr)	65690	65690	65690	27330	49570
Liquid Vol. Flow (barrel/day)	11860	11860	11860	3508	10610
Heat Flow	(Btu/hr)	-1.01E+08	1.05E+08	-1.08E+08	-2.76E+07	-9.61E+07

Table 13A: FIG. 4 Single-Unit Gas Separator Stream Properties

2016273827 12 Dec 2016

Property	209	210	211	212	213
Vapor Fraction	0.8048	0	0	1	0.8842
Temperature	(F)	-85.12	-85.02	-82.99	-85.02	-131.8
Pressure	(psig)	695	695	795	695	325
Molar Flow	(MMSCFD)	25.06	4.859	4.859	20.08	20.08
Mass Flow	(Ib/hr)	49570	11220	11220	38150	38150
Liquid Vol. Flow (barrel/day)	10610	2253	2253	8305	8305
Heat Flow	(Btu/hr)	-9.85E+07	-2.12E+07	-2.12E+07	-7.68E+07	-7.73E+07

Table 13B: FIG. 4 Single-Unit Gas Separator Stream Properties

Property	214	216	217	219
Vapor Fraction	1	1	1	1
Temperature	(F)	-65	80	107.7	236.8
Pressure	(psig)	320	317	377.4	800
Molar Flow	(MMSCFD)	20.08	20.08	20.08	20.08
Mass Flow	(Ib/hr)	38150	38150	38150	38150
Liquid Vol. Flow (barrel/day)	8305	8305	8305	8305
Heat Flow	(Btu/hr)	-7.49E+07	-7.19E+07	-7.14E+07	-6.89E+07

Table 13C: FIG. 4 Single-Unit Gas Separator Stream Properties

	201	206	219
Energy Content (Btu/ft3)	1395.72		1034.03
Vapor Pressure (psig)		250

Table 13D: FIG. 4 Single-Unit Gas Separator Stream Properties

Mole Frac	201	202	203	206	208	209	210
Nitrogen	0.0162*	0.0162	0.0162	0.0000	0.0174	0.0174	0.0066
CO2	0.0041*	0.0041	0.0041	0.0035	0.0049	0.0049	0.0078
Methane	0.7465*	0.7465	0.7465	0.0244	0.8815	0.8815	0.7287
Ethane	0.0822*	0.0822	0.0822	0.2120	0.0773	0.0773	0.1854
Propane	0.0608*	0.0608	0.0608	0.2910	0.0177	0.0177	0.0663
i-Butane	0.0187	0.0187	0.0187	0.0970	0.0007	0.0007	0.0033
n-Butane	0.0281	0.0281	0.0281	0.1462	0.0004	0.0004	0.0018
i-Pentane	0.0150	0.0150	0.0150	0.0781	0.0000	0.0000	0.0001
n-Pentane	0.0169	0.0169	0.0169	0.0880	0.0000	0.0000	0.0000
Hexane	0.0050	0.0050	0.0050	0.0260	0.0000	0.0000	0.0000
Heptane	0.0021	0.0021	0.0021	0.0109	0.0000	0.0000	0.0000
Octane	0.0044	0.0044	0.0044	0.0229	0.0000	0.0000	0.0000
Water	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
H2S	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000

Table 14A: FIG. 4 Single-Unit Gas Separator Stream Compositions

Mole Frac	211	212	213	214	216	217	219
Nitrogen	0.0066	0.0201	0.0201	0.0201	0.0201	0.0201	0.0201
CO2	0.0078	0.0042	0.0042	0.0042	0.0042	0.0042	0.0042
Methane	0.7287	0.9182	0.9182	0.9182	0.9182	0.9182	0.9182
Ethane	0.1854	0.0511	0.0511	0.0511	0.0511	0.0511	0.0511
Propane	0.0663	0.0062	0.0062	0.0062	0.0062	0.0062	0.0062
i-Butane	0.0033	0.0001	0.0001	0.0001	0.0001	0.0001	0.0001
n-Butane	0.0018	0.0001	0.0001	0.0001	0.0001	0.0001	0.0001
i-Pentane	0.0001	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
n-Pentane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Hexane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Heptane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Octane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Water	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
H2S	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000

Table 14B: FIG. 4 Single-Unit Gas Separator Stream Compositions

Energy Flow	301	302	303	304	306
Btu/hr	3,881,000	5,844,000	509,500	2,500,000	13,030

Table 15: FIG. 4 Single-Unit Gas Separator Energy Streams [0047] A second process simulation was performed using the single-unit gas separation process 160 shown in FIG. 4. The simulation was performed using the Aspen HYSYS Version

7.2 software package. This second simulation was run with a different feed composition. The material streams, their compositions, and the associated energy streams produced by the simulation are provided in Tables 16-18 below. The specified values are indicated by an asterisk (*). The physical properties are provided in degrees F, psig, MMSCFD, Ib/hr, barrel/day, Btu/ft³, and Btu/hr.

Property	201	202	203	206	208
Vapor Fraction	0.9458	0.8955	0.8594	0	1
Temperature	(F)	100'	19.52	-20	250.2	-83.96
Pressure	(psig)	600‘	595	590	555	550
Molar Flow	(MMSCFD)	10*	10	10	1.228	12.1
Mass Flow	(Ib/hr)	25190	25190	25190	8408	24190
Liquid Vol. Flow (barrel/day)	4570	4570	4570	988.6	5065
Heat Flow	(Btu/hr)	-4.20E+07	-4.35E+07	-4.42E+07	-8.37E+06	-5.06E+07

Table 16A: FIG. 4 Single-Unit Gas Separator Stream Properties

2016273827 12 Dec 2016

Property	209	210	211	212	213
Vapor Fraction	0.7243	0	0	1	0.8796
Temperature	(F)	-105.9	-105.9	103.9	-105.9	-175.2
Pressure	(psig)	545	545	645	545	130
Molar Flow	(MMSCFD)	12.1	3.326	3.326	8.774	8.774
Mass Flow	(lb/hr)	24190	7406	7406	16790	16790
Liquid Vol. Flow (barrel/day)	5065	1483	1483	3582	3582
Heat Flow	(Btu/hr)	-5.18E+07	-1.63E+07	-1.63E+07	-3.55E+07	-3.59E+07

Table 16B: FIG. 4 Single-Unit Gas Separator Stream Properties

Property	214	216	217	219
Vapor Fraction	1	1	1	1
Temperature	(F)	-90	80	129.4	353.1
Pressure	(psig)	125	122	168.8	600
Molar Flow	(MMSCFD)	8.774	8.774	8.774	8.774
Mass Flow	(lb/hr)	16790	16790	16790	16790
Liquid Vol. Flow (barrel/day)	3582	3582	3582	3582
Heat Flow	(Btu/hr)	-3.47E+07	-3.32E+07	-3.28E+07	-3.08E+07

Table 16C: FIG. 4 Single-Unit Gas Separator Stream Properties

	201	206	219
Energy Content (Btu/ft3)	1295		994
Vapor Pressure (psig)		200

Table 16D: FIG. 4 Single-Unit Gas Separator Stream Properties

Mole Frac	201	202	203	206	208	209	210
Nitrogen	0.0202*	0.0202	0.0202	0.0000	0.0186	0.0186	0.0069
CO2	0.0202*	0.0202	0.0202	0.0177	0.0289	0.0289	0.0509
Methane	0.808*	0.8080	0.8080	0.0156	0.8733	0.8733	0.7529
Ethane	0.0505*	0.0505	0.0505	0.1468	0.0774	0 0774	0.1838
Propane	0.0303*	0.0303	0.0303	0.2437	0.0016	0.0016	0.0050
i-Butane	0.0101*	0.0101	0.0101	0.0823	0.0000	0.0000	0.0000
n-Butane	0.0101*	0.0101	0.0101	0.0823	0.0000	0.0000	0.0000
i-Pentane	0.0101’	0.0101	0.0101	0.0823	0.0000	0.0000	0.0000
n-Pentane	0.0101*	0.0101	0.0101	0.0823	0.0000	0 0000	0.0000
Hexane	0.0101*	0.0101	0.0101	0.0823	0.0000	0.0000	0.0000
Heptane	0.0101*	0.0101	0.0101	0.0823	0.0000	0.0000	0.0000
Octane	0.0101*	0.0101	0.0101	0.0823	0.0000	0.0000	0.0000
Water	0*	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
H2S	0.0001*	0.0001	0.0001	0.0004	0.0002	0.0002	0,0004

Table 17A: FIG. 4 Single-Unit Gas Separator Stream Compositions

2016273827 12 Dec 2016

Mole Frac	211	212	213	214	216	217	219
Nitrogen	0.0069	0.0230	0.0230	0.0230	0.0230	0.0230	0.0230
CO2	0.0509	0.0206	0.0206	0.0206	0.0206	0.0206	0.0206
Methane	0.7529	0.9190	0.9190	0.9190	0.9190	0.9190	0.9190
Ethane	0.1838	0.0371	0.0371	0.0371	0.0371	0.0371	0.0371
Propane	0.0050	0.0003	0.0003	0.0003	0.0003	0.0003	0.0003
i-Butane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
n-Butane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
i-Pentane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
n-Pentane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Hexane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Heptane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Octane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Water	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
H2S	0.0004	0.0001	0.0001	0.0001	0.0001	0.0001	0.0001

Tabic 17B: FIG. 4 Single-Unit Gas Separator Stream Compositions

Energy Flow	301	302	303	304	306
Btu/hr	723,800	1,546,000	409,900	2,035,000	8,157

Table 18: FIG. 4 Single-Unit Gas Separator Stream Properties [0048] In another example, a process simulation was performed using the single-unit gas separation process 170 shown in FIG. 5. The simulation was performed using the Aspen HYSYS Version 7.2 software package. The material streams, their compositions, and the associated energy streams produced by the simulation are provided in Tables 19-21 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), British thermal units per standard cubic feet (Btu/ft³), and British thermal units per hour (Btu/hr).

Property	201	202	203	204	206	208
Vapor Fraction	0.9335	0.8517	0.7158	0.7087	0.0002	1
Temperature	(F)	100*	48.9	-15	-18	253.6	-55.46
Pressure	(psig)	800*	795	790	785	710	700
Molar Flow	(MMSCFD)	25*	25	25	25	4.775	25.62
Mass Flow	(Ib/hr)	65680	65680	65680	65680	27250	50700
Liquid Vol. Flow (barrel/day)	11860	11860	11860	11860	3491	10860
Heat Flow	(Btu/hr)	-1.01E+08	-1.04E+00	-1.08E+08	-1.08E+08	-2.75E+07	-9.83E+07

Table 19A: FIG. 5 Single-Unit Gas Separator Stream Properties

Property	209	210	211	212	213	214
Vapor Fraction	0.7893	0	0	1	0.8813	1
Temperature	(F)	-85.38	-85.39	-83.26	-85.39	-132.1	-65
Pressure	(psig)	695	695	795	695	325	320
Molar Flow	(MMSCFD)	25.62	5.399	5.399	20.23	20.23	20.23
Mass Flow	(Ib/hr)	50700	12280	12280	38440	38440	38440
Liquid Vol. Flow (barrel/day)	10860	2488	2488	8372	8372	8372
Heat Flow	(Btu/hr)	-1.01E+08	-2.34E+07	-2.34E+07	-7.74E+07	-7.79E+07	7.54E+07

Table 19B: FIG. 5 Single-Unit Gas Separator Stream Properties

Property	215	216	217	218	219
Vapor Fraction	1	1	1	1	1
Temperature	(F)	-58.02	80	107.5	120	256
Pressure	(psig)	315	312	371.1	366.1	800
Molar Flow	(MMSCFD)	20.23	20.23	20.23	20.23	20.23
Mass Flow	(Ib/hr)	38440	38440	38440	38440	38440
Liquid Vol. Flow (barrel/day)	8372	8372	8372	8372	8372
Heat Flow	(Btu/hr)	-7.53E+07	-7.24E+07	-7.19E+07	-7.16E+07	-6.89E+07

Table 19C: FIG. 5 Single-Unit Gas Separator Stream Properties

	201	206	219
Energy Content (Btu/ft3)	1395.72		1034.54
Vapor Pressure (psig)		250

Table 19D: FIG. 5 Single-Unit Gas Separator Stream Properties

Mole Frac	201	202	203	204	206	208	209	210	211
Nitrogen	0.0162*	0.0162	0.0162	0.0162	0.0000	0.0173	0.0173	0.0068	0.0068
CO2	0.0041*	0.0041	0.0041	0.0041	0.0043	0.0048	0.0048	0.0074	0.0074
Methane	0.7465*	0.7465	0.7465	0.7465	0.0225	0.8799	0.8799	0.7391	0.7391
Ethane	0.0822*	0.0822	0.0822	0.0822	0.2085	0.0800	0.0800	0.1837	0.1837
Propane	0.0608*	0.0608	0.0608	0.0608	0.2931	0.0176	0.0176	0.0610	0.0610
i-Butane	0.0187	0.0187	0.0187	0.0187	0.0978	0.0004	0.0004	0.0014	0.0014
n-Butane	0.0281	0.0281	0.0281	0.0281	0.1471	0.0001	0.0001	0.0006	0.0006
i-Pentane	0.0150	0.0150	0.0150	0.0150	0.0785	0.0000	0.0000	0.0000	0.0000
n-Pentane	0.0169	0.0169	0.0169	0.0169	0.0883	0.0000	0.0000	0.0000	0.0000
Hexane	0.0050	0.0050	0.0050	0.0050	0.0260	0.0000	0.0000	0.0000	0 0000
Heptane	0.0021	0.0021	0.0021	0.0021	0.0108	0.0000	0.0000	0.0000	0.0000
Octane	0.0044	0.0044	0.0044	0.0044	0.0231	0.0000	0.0000	0.0000	0.0000
Water	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
H2S	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000

Table 20A: FIG. 5 Single-Unit Gas Separator Stream Compositions

2016273827 12 Dec 2016

Mole Frac	212	213	214	215	216	217	218	219
Nitrogen	0.0201	0.0201	0.0201	0.0201	0.0201	0.0201	0.0201	0.0201
CO2	0.0041	0.0041	0.0041	0.0041	0.0041	0.0041	0.0041	0.0041
Methane	0.9175	0.9175	0.9175	0.9175	0.9175	0.9175	0.9175	0.9175
Ethane	0.0524	0.0524	0.0524	0.0524	0.0524	0.0524	0.0524	0.0524
Propane	0.0059	0.0059	0.0059	0.0059	0.0059	0.0059	0.0059	0.0059
i-Butane	0.0001	0.0001	0.0001	0.0001	0.0001	0.0001	0.0001	0.0001
n-Butane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0 0000
i-Pentane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0 0000
n-Pentane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Hexane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Heptane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0 0000
Octane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Water	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	00000
H2S	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000

Table 20B: FIG. 5 Single-Unit Gas Separator Stream Compositions

Energy Flow	301	302	303	304	306
Btu/hr	3,694,000	5,772,000	510,100	2,695,000	14,600

Table 21: FIG. 5 Single-Unit Gas Separator Energy Streams [0049] A second process simulation was performed using the single-unit gas separation process 170 shown in FIG. 5. The simulation was performed using the Aspen HYSYS Version

7.2 software package. This second simulation was run with a different feed composition. The material streams, their compositions, and the associated energy streams produced by the simulation are provided in Tables 22-24 below. The specified values are indicated by an asterisk (*). The physical properties are provided in degrees F, psig, MMSCFD, Ib/hr, barrel/day,

Btu/ft³, and Btu/hr.

Property	201	202	203	204	206	208
Vapor Fraction	1	0.9627	0.7875	0.7796	0.0002	1
Temperature	(F)	100*	41.32	-15	-17	226.3	19.08
Pressure	(psig)	800*	795	790	785	710	700
Molar Flow	(MMSCFD)	25*	25	25	25	2.572	28.32
Mass Flow	(Ib/hr)	59670	59670	59670	59670	13130	62320
Liquid Vol. Flow (barrel/day)	11600	11600	11600	11600	1776	12860
Heat Flow	(Btu/hr)	-9.54E+07	-9.80E+07	-1.02E+08	-1.02E+08	-1.36E+07	-1.09E+08

Table 22A: FIG. 5 Single-Unit Gas Separator Stream Properties

2016273827 12 Dec 2016

Property	209	210	211	212	213	214
Vapor Fraction	0.7925	0	0	1	0.898	1
Temperature	(F)	-44.81	-44.96	-43.02	-44.96	-92.48	-30
Pressure	(psig)	695	695	795	695	300	295
Molar Flow	(MMSCFD)	28.32	5.888	5.888	22.43	22.43	22.43
Mass Flow	(Ib/hr)	62320	15780	15780	46530	46530	46530
Liquid Vol. Flow (barrel/day)	12860	3035	3035	9823	9823	9823
Heat Flow	(Btu/hr)	-1.12E+08	-2.61 E+07	2.61 E+07	-8.60E+07	-8.68E+07	-8.41 E+07

Table 22B: FIG. 5 Single-Unit Gas Separator Stream Properties

Property	215	216	217	218	219
Vapor Fraction	1	1	1	1	1
Temperature	(F)	-25.68	80	116.7	120	202.8
Pressure	(psig)	290	287	365.4	3604	600
Molar Flow	(MMSCFD)	22.43	22.43	22.43	22.43	22.43
Mass Flow	(Ib/hr)	46530	46530	46530	46530	46530
Liquid Vol. Flow (barrel/day)	9823	9823	9823	9823	9823
Heat Flow	(Btu/hr)	-8.40E+07	-8.14E+07	-8.06E+07	-8.05E+07	-7.87E+07

Table 22C: FIG. 5 Single-Unit Gas Separator Stream Properties

	201	206	219
Energy Content (Btu/ft3)	1299.9		1118
Vapor Pressure (psig)		200

Table 22D: FIG. 5 Single-Unit Gas Separator Stream Properties

Mole Frac	201	202	203	204	206	208	209	210	211
Nitrogen	0.0158*	0.0158	0.0158	0.0158	0.0000	0.0148	0.0148	0.0043	0.0043
CO2	0.004*	0.0040	0.0040	0.0040	0.0003	0.0047	0.0047	0.0059	0.0059
Methane	0.7266*	0.7266	0.7266	0.7266	0.0046	0.7430	0.7430	0.4902	0.4902
Ethane	0.1616*	0.1616	0.1616	0.1616	0.2329	0.2066	0.2066	0.4091	0.4091
Propane	0.0592*	0.0592	0.0592	0.0592	0.4941	0.0228	0.0228	0.0744	0.0744
i-Butane	0.0059*	0.0059	0.0059	0.0059	0.0565	0.0002	0.0002	0.0008	0.0008
n-Butane	0.0111*	0.0111	0.0111	0.0111	0.1077	0.0001	0.0001	0.0005	0.0005
i-Pentane	0.0025*	0.0025	0.0025	0.0025	0.0243	0.0000	0.0000	0.0000	0.0000
n-Pentane	0.0034*	0.0034	0.0034	0.0034	0.0333	0.0000	0.0000	0.0000	0.0000
Hexane	0.0018*	0.0018	0.0018	0.0018	0.0175	0.0000	0.0000	0.0000	0.0000
Heptane	0.001*	0.0010	0.0010	0.0010	0.0097	0.0000	0.0000	0.0000	0.0000
Octane	0.001*	0.0010	0.0010	0.0010	0.0097	0.0000	0.0000	0.0000	0.0000
Water	0*	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
H2S	0.0062*	0.0062	0.0062	0.0062	0.0097	0.0077	0.0077	0.0148	0.0148

Table 23A: FIG. 5 Single-Unit Gas Separator Stream Compositions

2016273827 12 Dec 2016

Mole Frac	212	213	214	215	216	217	218	219
Nitrogen	0.0176	0.0176	0.0176	0.0176	0.0176	0.0176	0.0176	0.0176
CO2	0.0044	0.0044	0.0044	0.0044	0.0044	0.0044	0.0044	0.0044
Methane	0.8099	0.8099	0.8099	0.8099	0.8099	0.8099	0.8099	0.8099
Ethane	0.1529	0.1529	0.1529	0.1529	0.1529	0.1529	0.1529	0.1529
Propane	0.0093	0.0093	0.0093	0.0093	0.0093	0.0093	0.0093	0.0093
i-Butane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
n-Butane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
i-Pentane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
n-Pentane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Hexane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Heptane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Octane	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
Water	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000	0.0000
H2S	0.0058	0.0058	0.0058	0.0058	0.0058	0.0058	0.0058	0.0058

Table 23B: FIG. 5 Single-Unit Gas Separator Stream Compositions

Energy Flow	301	302	303	304	306
Btu/hr	3,533,000	4,773,000	784,200	1,854,000	16,660

Table 24: FIG. 5 Single-Unit Gas Separator Energy Streams [0050] At least one embodiment is disclosed and variations, combinations, and/or modifications of the embodiment(s) and/or features of the embodiment(s) made by a person having ordinary skill in the art are within the scope of the disclosure. Alternative embodiments that result from combining, integrating, and/or omitting features of the embodiment(s) are also within the scope of the disclosure. Where numerical ranges or limitations are expressly slated, 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 I to about 10 includes, 2, 3, 4, etc.; greater than 0.10 includes 0.11, 0.12, 0.13, etc.). For example, whenever a numerical range with a lower limit, R|, and an upper limit, R_u, is disclosed, any number falling within the range is specifically disclosed. In particular, the following numbers within the range are specifically disclosed: R = R, + k * (R_u - R|), wherein k is a variable ranging from 1 percent to 100 percent with a 1 percent increment, i.e., k is I percent, 2 percent, 3 percent. 4 percent, 5 percent, ... 50 percent, 51 percent, 52 percent, .... 95 percent, 96 percent, 97 percent, 98 percent, 99 percent, or 100 percent. All percentages used herein are weight percentages unless otherwise indicated. Moreover, any numerical range defined by two R numbers as defined in the above is also specifically disclosed. Use of broader terms such as comprises, includes, and having should be understood to provide support for narrower terms such as consisting of, consisting essentially of, and comprised substantially of. All documents described herein are incorporated herein by reference.

Throughout this specification and the claims which follow, unless the context requires otherwise, the word comprise, and variations such as comprises and comprising, will be understood to imply the inclusion of a stated integer or step or group of integers or steps but not the exclusion of any other integer or step or group of integers or steps.

The reference in this specification to any prior publication (or information derived from it), or to any matter which is known, is not, and should not be taken as an acknowledgment or admission or any form of suggestion that that prior publication (or information derived from it) or known matter forms part of the common general knowledge in the field of endeavour to which this specification relates.

Claims (20)

1. THE CLAIMS DEFINING THE INVENTION ARE AS FOLLOWS:

   1. An apparatus comprising:

   a multi-stage separation column configured to separate a hydrocarbon feed stream into a top effluent stream and a liquefied petroleum gas (LPG)-rich stream;

   an expander configured to expand the top effluent stream and produce a natural gas-rich stream;

   a compressor configured to compress the natural gas-rich stream;

   a first heat exchanger configured to partially condense the top effluent stream into a vapor portion and a liquid portion;

   a reflux separator configured to separate the vapor portion from the liquid portion;

   a second heat exchanger configured to cool the hydrocarbon feed stream using the natural gas-rich stream; and a third heat exchanger configured to cool the hydrocarbon feed stream using mechanical refrigeration, wherein the liquid portion is returned to the multi-stage separation column as reflux, wherein the multi-stage separation column and the reflux separator are the only two separators in the apparatus, wherein the expander is a Joule-Thomson expander, and wherein the Joule-Thompson expander receives the vapor portion from the reflux separator and feeds an expanded natural gas-rich stream to the first heat exchanger.
2. 2. The apparatus of claim 1, further comprising a fourth heat exchanger configured to cool the hydrocarbon feed stream using the natural gas-rich stream, wherein the hydrocarbon feed stream contacts the fourth heat exchanger, then the third heat exchanger, and then the second heat exchanger prior to entering the multi-stage separation column, wherein the composition of the hydrocarbon feed stream is substantially the same as the natural gas in a hydrocarbon formation from which the hydrocarbon feed stream

   C:\Interwoven\NRPortbl\DCC\MDT\18619915_l.doc - 18/04/19

   2016273827 18 Apr 2019 originated, and wherein the LPG-rich steam has a vapor pressure from about 200 pounds per a square inch gauge (psig) to about 300 psig.
3. 3. The apparatus of claim 1 or claim 2, further comprising a pump coupled between the reflux separator and the multi-stage separation column, wherein the pump is configured to control a rate at which the reflux is fed back to the multi-stage separation column, and wherein no cryogenic conditions are used.
4. 4. The apparatus of any one of claims 1 to 3, wherein the expander is configured to generate energy as the expander expands the top effluent stream and produces the natural gasrich stream, wherein the energy is supplied to the compressor and is used to compress the natural gas-rich stream, wherein the multi-stage separation column operates at a pressure range of about 390 - about 795 pounds per a square inch gauge, and wherein the multi-stage separation column operates at a temperature range of about -80 degrees Fahrenheit (°F) about 100 °F.
5. 5. The apparatus of any one of claims 1 to 4, further comprising a second compressor configured to:

   receive the natural gas-rich stream;

   increase a pressure of the natural gas-rich stream; and transfer the natural gas-rich stream to a pipeline.
6. 6. The apparatus of any one of claims 1 to 5, further comprising a reboiler coupled to the multi-stage separation column and produce a boil-up stream and the LPG-rich stream.
7. 7. The apparatus of any one of claims 1 to 6, further comprising an air cooler configured to receive and cool the natural gas-rich stream.
8. 8. A method comprising:

   C:\Interwoven\NRPortbl\DCC\MDT\19145210_l.doc - 6/08/19

   2016273827 06 Aug 2019 separating a hydrocarbon feed stream into a top effluent stream and a liquefied petroleum gas (LPG)-rich stream;

   expanding the top effluent stream to produce a natural gas-rich stream by receiving a vapor portion from a reflux separator at a Joule-Thompson expander and producing an expanded natural gas-rich stream with the Joule-Thompson expander;

   feeding the expanded natural gas-rich stream from the Joule-Thompson expander to a first heat exchanger partially condensing the top effluent stream into the vapor portion and a liquid portion; separating the vapor portion from the liquid portion;

   cooling the hydrocarbon feed stream using the natural gas-rich stream; and cooling the hydrocarbon feed stream using mechanical refrigeration.
9. 9. The method according to claim 8, further comprising returning the liquid portion to a multi-stage separation column as reflux, and wherein the LPG-rich steam has a vapor pressure from about 200 pounds per a square inch gauge (psig) to about 300 psig.
10. 10. The method according to claim 8 or 9, further comprising cooling the hydrocarbon feed stream using the natural gas-rich stream, wherein no cryogenic conditions are used.
11. 11. The method according to any one of claims 8 to 10, further comprising receiving the hydrocarbon feed stream from a hydrocarbon formation wherein the hydrocarbon stream is separated into the top effluent stream and the LPG-rich stream in a multi-stage separation column, wherein the multi-stage separation column operates at a pressure range of about 390 about 795 pounds per a square inch gauge, and wherein the multi-stage separation column operates at a temperature range of about -80 degrees Fahrenheit (°F) - about 100 °F.
12. 12. The method according to any one of claims 8 to 11, further comprising controlling a rate at which the reflux is returned to a multi-stage separation column using a pump.

    C:\Interwoven\NRPortbl\DCC\MDT\18619915_l.doc - 18/04/19

    2016273827 18 Apr 2019
13. 13. The method according to any one of claims 8 to 12, wherein expanding the top effluent stream to produce the natural gas-rich stream comprises generating energy that is used to power a compressor.
14. 14. The method according to any one of claims 8 to 13, further comprising: receiving the natural gas-rich stream;

    increasing a pressure of the natural gas-rich stream; and transferring the natural gas-rich stream to a pipeline.
15. 15. The method according to any one of claims 8 to 14, further comprising reboiling the LPG-rich stream from the multi-stage separation column to produce a boil-up stream that is fed back to the multi-stage separation column.
16. 16. The method according to any one of claims 8 to 15, further comprising cooling the natural-gas rich stream in an air cooler.
17. 17. A set of process equipment comprising:

    first piping configured to receive a hydrocarbon feed stream from a hydrocarbon formation;

    a multi-stage separation column coupled to the first piping and configured to separate the hydrocarbon feed stream into a top effluent stream and a liquefied petroleum gas (LPG)rich stream;

    second piping configured to receive the top effluent stream from the multi-stage separation column;

    a first heat exchanger coupled to the second piping and configured to partially condense the top effluent stream into a vapor portion and a liquid portion;

    a reflux separator coupled to the first heat exchanger and configured to separate the vapor portion from the liquid portion, wherein the multi-stage separation column and the reflux separator are the only two separators in the set of process equipment; and

    C:\Interwoven\NRPortbl\DCC\MDT\18619915_l.doc - 18/04/19

    2016273827 18 Apr 2019 a Joule-Thomson expander coupled to the reflux separator and configured to receive the vapor portion from the reflux separator, produce an expanded natural gas-rich stream, and feed the expanded natural gas-rich stream to the first heat exchanger.
18. 18. The set of process equipment according to claim 17, further comprising third piping configured to transfer the natural gas rich-stream to a pipeline, and wherein the LPG-rich steam has a vapor pressure from about 200 pounds per a square inch gauge (psig) to about 300 psig.
19. 19. The set of process equipment according to claim 17 or 18, further comprising a series of heat exchangers configured to cool the hydrocarbon stream before transferring the hydrocarbon feed stream to the multi-stage separation column, and wherein no cryogenic conditions are used.
20. 20. The set of process equipment according to any one of claims 17 to 19, further comprising a pump coupled between the reflux separator and the multi-stage separation column, wherein the pump is configured to control a rate at which reflux is returned to the multi-stage separation column, wherein the multi-stage separation column operates at a pressure range of about 390 - about 795 pounds per a square inch gauge, and wherein the multi-stage separation column operates at a temperature range of about -80 degrees Fahrenheit (°F)-about 100 °F.