# US 9,752,826 B2 · NGL recovery from a recycle stream having natural gas

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- Number: US 9,752,826 B2
- Document ID: US9752826B2
- Status: Granted
- Kind: B2
- Application number: 13/946,773
- Filed: 2013-07-19
- Published: 2013-11-14
- Granted: 2017-09-05
- Earliest claimed: 2007-05-18
- Assignees: Pilot Energy Solutions, LLC
- Applicants: Pilot Energy Solutions, LLC
- Inventors: Eric Prim
- Web page: https://patentgrep.com/patent/US9752826B2

## CPC

- F25J 3/0204: {characterised by the feed stream (for air F25J3/04)}
- C10L 3/104: {Carbon dioxide}
- F25J 3/0209: {Natural gas or substitute natural gas}
- F25J 3/0233: {separation of CnHm with 1 carbon atom or more}
- F25J 3/0242: {separation of CnHm with 3 carbon atoms or more}
- F25J 3/0266: {separation of carbon dioxide (production of carbon dioxide in general C01B32/00)}
- F25J 3/044: {using a single pressure main column system only (F25J3/0446, F25J3/04624, F25J3/04636 take precedence)}
- F25J 2200/02: in a single pressure main column system
- F25J 2200/74: Refluxing the column with at least a part of the partially condensed overhead gas
- F25J 2205/04: in the feed line, i.e. upstream of the fractionation step
- F25J 2215/04: Recovery of liquid products
- F25J 2215/80: Carbon dioxide
- F25J 2220/02: Separating impurities in general from the feed stream
- F25J 2220/64: Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
- F25J 2220/66: Separating acid gases, e.g. CO2, SO2, H2S or RSH
- F25J 2220/68: Separating water or hydrates
- F25J 2260/80: Integration in an installation using carbon dioxide, e.g. for EOR, sequestration, refrigeration etc.
- F25J 2290/10: Mathematical formulae, modeling, plot or curves; Design methods
- Y02C 20/40: of CO2
- F25J: LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS {OR LIQUEFIED GASEOUS} MIXTURES BY PRESSURE AND COLD TREATMENT {OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE (cryogenic pumps F04B37/08; gas storage vessels, gas holders F17; filing vessels with, or discharging from vessels, compressed, liquefied or solidified gases F17C; refrigeration machines, plants, or systems F25B)}
- C10L: FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
- Y02C: CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]

## Abstract

A method for recovering natural gas liquids from a recycle stream having natural gas is provided. In one embodiment, a carbon dioxide recycle stream that comprises carbon dioxide, natural gas, and natural gas liquids is received. The carbon dioxide recycle stream is separated into a purified carbon dioxide recycle stream and a natural gas liquids stream. The purified carbon dioxide recycle stream comprises the carbon dioxide and the natural gas, and the natural gas liquids stream comprises the natural gas liquids. In another embodiment, a system comprises piping and a separator. The piping is configured to receive a recycle stream, and the separator is coupled to the piping and is configured to separate the recycle stream into a purified recycle stream and a natural gas liquids stream.

## Claims

### Claim 1

A method comprising:
receiving a feed stream, wherein the feed stream comprises carbon dioxide, C1 to C2 hydrocarbons, C3 to C8 hydrocarbons, C9+ hydrocarbons, branched hydrocarbons, and aromatic hydrocarbons;
separating the feed stream into a heavy hydrocarbon stream and a carbon dioxide recycle stream in a separator, wherein the heavy hydrocarbon stream comprises substantially all of the C9+ hydrocarbons, the branched hydrocarbons, and the aromatic hydrocarbons from the feed stream, wherein the heavy hydrocarbon stream comprises substantially none of the carbon dioxide and the C1 to C2 hydrocarbons from the feed stream, and wherein the carbon dioxide recycle stream comprises substantially all of the carbon dioxide and the C1 to C2 hydrocarbons from the feed stream;
separating the carbon dioxide recycle stream into a purified carbon dioxide recycle stream and a natural gas liquids stream in a distillation column, wherein the purified carbon dioxide recycle stream comprises the carbon dioxide and the C1 to C2 hydrocarbons, wherein the natural gas liquids stream comprises the C3 to C8 hydrocarbons, wherein the purified carbon dioxide recycle stream comprises substantially all of the C2 hydrocarbons from the carbon dioxide recycle stream and the natural gas liquids stream comprises substantially none of the C2 hydrocarbons from the carbon dioxide recycle stream, and wherein the purified carbon dioxide recycle stream comprises substantially none of the C3 hydrocarbons from the carbon dioxide recycle stream and the natural gas liquids stream comprises substantially all of the C3 hydrocarbons from the carbon dioxide recycle stream;
compressing the carbon dioxide recycle stream in a first compressor as the carbon dioxide recycle stream is passed from the separator to a dehydrator;
dehydrating the carbon dioxide recycle stream in the dehydrator as the carbon dioxide recycle stream is passed from the separator to the distillation column;
compressing the purified carbon dioxide recycle stream in a second compressor as the purified carbon dioxide recycle stream is passed from the distillation column to an injection well;
cooling the carbon dioxide recycle stream in a heat exchanger using the purified carbon dioxide recycle stream, wherein the carbon dioxide recycle stream passes from the dehydrator through the heat exchanger to the distillation column, and wherein the purified carbon dioxide recycle stream passes from a condenser of the distillation column through the heat exchanger to the second compressor;
receiving a sour natural gas liquids rich stream from the distillation column at a second heat exchanger;
cooling the sour natural gas liquids rich stream through the second heat exchanger;
passing the cool sour natural gas liquids rich stream from the second heat exchanger to an expansion valve;
reducing the pressure of the cool sour natural gas liquids rich stream in the expansion valve to produce a low pressure cool sour natural gas liquids rich stream; and
separating the low pressure cool sour natural gas liquids rich stream in a second separator to produce an H2S stream and a sweetened natural gas liquids rich stream.

### Claim 2 (depends on 1)

The method according to claim 1, wherein the carbon dioxide recycle stream separated in the distillation column and the natural gas liquids stream are substantially free of C9+ hydrocarbons, wherein the purified carbon dioxide recycle stream comprises at least 90 molar % of the C1 to C2 hydrocarbons from the carbon dioxide recycle stream, wherein the natural gas liquids stream comprises at least 70 molar % of the C3 to C8 hydrocarbons from the carbon dioxide recycle stream, wherein the distillation column comprises the condenser and a reboiler, wherein the purified carbon dioxide recycle stream is generated by the condenser, and wherein the natural gas liquids stream is generated by the reboiler.

### Claim 3 (depends on 1)

The method according to claim 1, wherein the carbon dioxide recycle stream comprises acid gas, and wherein separating the carbon dioxide recycle stream into the purified carbon dioxide recycle stream and the natural gas liquids stream comprises separating the acid gas into the natural gas liquids stream.

### Claim 4 (depends on 1)

The method according to claim 1, wherein separating the carbon dioxide recycle stream into the purified carbon dioxide recycle stream and the natural gas liquids stream consists essentially of:
receiving the carbon dioxide recycle stream at a separation column;
reboiling a portion of the carbon dioxide recycle stream received from the separation column with a reboiler to generate the natural gas liquids stream; and
condensing another portion of the carbon dioxide recycle stream received from the separation column with the condenser to generate the purified carbon dioxide recycle stream.

### Claim 5

A system comprising:
first piping configured to receive a feed stream, wherein the feed stream comprises an injection gas, C1 to C2 hydrocarbons, C3 to C8 hydrocarbons, C9+ hydrocarbons, branched hydrocarbons, and aromatic hydrocarbons;
a separator coupled to the first piping and configured to separate the feed stream into a heavy hydrocarbon stream and a recycle stream, wherein the heavy hydrocarbon stream comprises substantially all of the C9+ hydrocarbons, the branched hydrocarbons, and the aromatic hydrocarbons from the feed stream, wherein the heavy hydrocarbon stream comprises substantially none of the injection gas and the C1 to C2 hydrocarbons from the feed stream, and wherein the recycle stream comprises substantially all of the injection gas and the C1 to C2 hydrocarbons from the feed stream;
second piping configured to receive the recycle stream from the separator;
a distillation column coupled to the second piping and configured to separate the recycle stream into a purified recycle stream and a natural gas liquids stream, wherein the purified recycle stream comprises the injection gas and the C1 to C2 hydrocarbons, wherein the natural gas liquids stream comprises the C3 to C8 hydrocarbons, wherein the purified recycle stream comprises substantially all of the C2 hydrocarbons from the recycle stream and the natural gas liquids stream comprises substantially none of the C2 hydrocarbons from the recycle stream, and wherein the purified recycle stream comprises substantially none of the C3 hydrocarbons from the recycle stream and the natural gas liquids stream comprises substantially all of the C3 hydrocarbons from the recycle stream;
a first compressor configured to compress the recycle stream as the recycle stream is passed from the separator to a dehydrator;
the dehydrator configured to dehydrate the recycle stream as the recycle stream is passed from the separator to the distillation column;
a second compressor configured to compress the purified recycle stream as the purified recycle stream is passed from the distillation column to an injection well;
a heat exchanger configured to cool the recycle stream using the purified recycle stream, wherein the recycle stream passes from the dehydrator through the heat exchanger to the distillation column, and wherein the purified recycle stream passes from a condenser of the distillation column through the heat exchanger to the second compressor;
a second heat exchanger that receives a sour natural gas liquids rich stream from the distillation column and that cools the sour natural gas liquids rich stream;
an expansion valve that receives the cool sour natural gas liquids rich stream from the second heat exchanger and that reduces the pressure of the cool sour natural gas liquids rich stream to produce a low pressure cool sour natural gas liquids rich stream; and
a second separator that separates the low pressure cool sour natural gas liquids rich stream to produce an H2S stream and a sweetened natural gas liquids rich stream.

### Claim 6 (depends on 5)

The system according to claim 5, wherein the system is configured to cool the recycle stream with the purified recycle stream before separating the recycle stream into the purified recycle stream and the natural gas liquids stream, wherein the recycle stream and the natural gas liquids stream are substantially free from C9+ hydrocarbons, wherein the purified recycle stream comprises at least 90 molar % of the C1 to C2 hydrocarbons from the recycle stream, wherein the natural gas liquids stream comprises at least 70 molar % of the C3 to C8 hydrocarbons from the recycle stream, wherein the distillation column comprises the condenser and a reboiler, wherein the purified recycle stream is generated by the condenser, and wherein the natural gas liquids stream is generated by the reboiler.

### Claim 7 (depends on 5)

The system according to claim 5, wherein the system is configured to add a makeup stream to the purified recycle stream to form an injection stream, and wherein the makeup stream comprises carbon dioxide, nitrogen, methane, ethane, air, or water.

### Claim 8 (depends on 5)

The system according to claim 5, wherein the distillation column consists essentially of a separation column, a reboiler, and the condenser, wherein the separation column receives the recycle stream, wherein the reboiler receives a first portion of the recycle stream from the separation column and generates the natural gas liquids stream, and wherein the condenser receives a second portion of the recycle stream from the separation column and generates the purified recycle stream.

### Claim 9

A set of process equipment comprising:
a first input line configured to receive a feed stream, wherein the feed stream comprises an injection gas, C1 to C2 hydrocarbons, C3 to C8 hydrocarbons, C9+ hydrocarbons, branched hydrocarbons, and aromatic hydrocarbons;
a separator coupled to the first input line and configured to separate the feed stream into a heavy hydrocarbon stream and a recycle stream, wherein the heavy hydrocarbon stream comprises substantially all of the C9+ hydrocarbons, the branched hydrocarbons, and the aromatic hydrocarbons from the feed stream, wherein the heavy hydrocarbon stream comprises substantially none of the injection gas and the C1 to C2 hydrocarbons from the feed stream, and wherein the recycle stream comprises substantially all of the injection gas and the C1 to C2 hydrocarbons from the feed stream;
a second input line configured to receive the recycle stream from the separator;
a distillation column configured to receive the recycle stream from the second input line and separate the recycle stream into a purified recycle stream and a natural gas liquids stream;
a first output line configured to output the purified recycle stream from the distillation column, wherein the purified recycle stream comprises the injection gas and the C1 to C2 hydrocarbons;
a second output line configured to output the natural gas liquids stream from the distillation column, wherein the natural gas liquids stream comprises the C3 to C8 hydrocarbons, wherein the purified recycle stream comprises substantially all of the C2 hydrocarbons from the recycle stream and the natural gas liquids stream comprises substantially none of the C2 hydrocarbons from the recycle stream, and wherein the purified recycle stream comprises substantially none of the C3 hydrocarbons from the recycle stream and the natural gas liquids stream comprises substantially all of the C3 hydrocarbons from the recycle stream;
a first compressor configured to compress the recycle stream as the recycle stream is passed from the separator to a dehydrator;
the dehydrator configured to dehydrate the recycle stream as the recycle stream is passed from the separator to the distillation column;
a second compressor configured to compress the purified recycle stream as the purified recycle stream is passed from the distillation column to an injection well;
a heat exchanger configured to cool the recycle stream using the purified recycle stream, wherein the recycle stream passes from the dehydrator through the heat exchanger to the distillation column, and wherein the purified recycle stream passes from a condenser of the distillation column through the heat exchanger to the second compressor;
a second heat exchanger that receives a sour natural gas liquids rich stream from the distillation column and that cools the sour natural gas liquids rich stream;
an expansion valve that receives the cool sour natural gas liquids rich stream from the second heat exchanger and that reduces the pressure of the cool sour natural gas liquids rich stream to produce a low pressure cool sour natural gas liquids rich stream; and
a second separator that separates the low pressure cool sour natural gas liquids rich stream to produce an H2S stream and a sweetened natural gas liquids rich stream.

### Claim 10 (depends on 9)

The set of process equipment according to claim 9, wherein the recycle stream and the natural gas liquids stream are substantially free from C9+ hydrocarbons, wherein the purified recycle stream comprises at least 90 molar % of the C1 to C2 hydrocarbons from the recycle stream, wherein the natural gas liquids stream comprises at least 70 molar % of the C3 to C8 hydrocarbons from the recycle stream, wherein the distillation column comprises the condenser and a reboiler, wherein the purified recycle stream is generated by the condenser, and wherein the natural gas liquids stream is generated by the reboiler.

### Claim 11 (depends on 9)

The set of process equipment according to claim 9, wherein each of the separator and the second separator comprises a phase separator or a column, wherein the heavy hydrocarbon stream comprises C9+ hydrocarbons, branched hydrocarbons, or aromatic hydrocarbons, and wherein the acid gas stream comprises carbon dioxide or hydrogen sulfide.

### Claim 12 (depends on 9)

The set of process equipment according to claim 9, wherein the injection gas comprises carbon dioxide, nitrogen, methane, ethane, air, or water.

### Claim 13 (depends on 9)

The set of process equipment according to claim 9, wherein the distillation column consists essentially of a separation column, a reboiler, and the condenser, wherein the separation column receives the recycle stream, wherein the reboiler receives a first portion of the recycle stream from the separation column and generates the natural gas liquids stream, and wherein the condenser receives a second portion of the recycle stream from the separation column and generates the purified recycle stream.

### Claim 14 (depends on 1)

The method according to claim 1, wherein the first compressor increases an energy level of the carbon dioxide recycle stream by at least 50%, wherein the dehydrator dehydrates the carbon dioxide recycle stream such that after passing through the dehydrator the carbon dioxide recycle stream is substantially free of water, and wherein the second compressor increases an energy level of the purified carbon dioxide recycle stream by at least 50%.

### Claim 15 (depends on 5)

The system according to claim 5, wherein the first compressor increases an energy level of the recycle stream by at least 50%, wherein the dehydrator dehydrates the recycle stream such that after passing through the dehydrator the recycle stream is substantially free of water, and wherein the second compressor increases an energy level of the purified recycle stream by at least 50%.

### Claim 16 (depends on 9)

The set of process equipment according to claim 9, wherein the first compressor increases an energy level of the recycle stream by at least 50%, wherein the dehydrator dehydrates the recycle stream such that after passing through the dehydrator the recycle stream is substantially free of water, and wherein the second compressor increases an energy level of the purified recycle stream by at least 50%.

### Claim 17 (depends on 1)

The method according to claim 1, further comprising adding a carbon dioxide makeup stream to the purified carbon dioxide recycle stream at the second compressor.

### Claim 18 (depends on 5)

The system according to claim 5, wherein a carbon dioxide makeup stream is added to the purified recycle stream at the second compressor.

### Claim 19 (depends on 9)

The set of process equipment according to claim 9, wherein a carbon dioxide makeup stream is added to the purified recycle stream at the second compressor.