# US 10,371,441 B2 · Hydrocarbon condensate stabilizer and a method for producing a stabilized hydrocarbon condensate stream

> Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt

- Number: US 10,371,441 B2
- Document ID: US10371441B2
- Status: Granted
- Kind: B2
- Application number: 15/326,960
- Filed: 2015-07-09
- Published: 2017-07-06
- Granted: 2019-08-06
- Earliest claimed: 2014-07-24
- Assignees: Shell Oil Company
- Applicants: Shell Oil Company
- Inventors: Lars Hendrik Van Leeuwen; Micha Hartenhof; Divya Jain
- Web page: https://patentgrep.com/patent/US10371441B2

## CPC

- F25J 1/0022: {Hydrocarbons, e.g. natural gas}
- C10G 5/06: by cooling or compressing
- C10G 7/02: Stabilising gasoline by removing gases by fractioning
- C10L 1/04: essentially based on blends of hydrocarbons
- C10L 3/06: Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04 {(liquefying by pressure and cold treatment F25J)}
- F25J 1/0035: {by gas expansion with extraction of work}
- F25J 1/0042: {by liquid expansion with extraction of work}
- F25J 1/0231: {for the working-up of the hydrocarbon feed, e.g. reinjection of heavier hydrocarbons into the liquefied gas}
- F25J 3/0209: {Natural gas or substitute natural gas}
- F25J 3/0233: {separation of CnHm with 1 carbon atom or more}
- F25J 3/0247: {separation of CnHm with 4 carbon atoms or more}
- C10G 2300/1025: Natural gas
- C10L 2290/06: Heat exchange, direct or indirect
- C10L 2290/46: Compressors or pumps
- C10L 2290/48: Expanders, e.g. throttles or flash tanks
- C10L 2290/543: Distillation, fractionation or rectification for separating fractions, components or impurities during preparation or upgrading of a fuel
- 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 2205/02: using simple phase separation in a vessel or drum
- F25J 2205/04: in the feed line, i.e. upstream of the fractionation step
- F25J 2220/64: Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
- F25J 2230/24: Multiple compressors or compressor stages in parallel
- F25J 2230/30: Compression of the feed stream
- F25J 2230/60: the fluid being hydrocarbons or a mixture of hydrocarbons
- F25J 2240/02: Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
- F25J 2240/40: Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
- F25J 2260/20: Integration in an installation for liquefying or solidifying a fluid stream
- 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)}
- C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- 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

## Abstract

A mixed phase pressurized unstabilized hydrocarbon stream is fed into a stabilizer column at a feed pressure. A liquid phase of stabilized hydrocarbon condensate is discharged from a bottom end of the stabilizer column, while a vapor phase of volatile components from the pressurized unstabilized hydrocarbon condensate stream is discharged from a top end of the stabilizer column. The vapor phase being discharged from the top end of the stabilizer column is compressed and subsequently passed through an ambient heat exchanger wherein partial condensation takes place. The resulting partially condensed overhead stream is separated in an overhead separator into a vapor effluent stream and an overhead liquid stream. After discharging the overhead liquid stream from the overhead separator, it is selectively divided into a liquid reflux stream and a liquid effluent stream. The liquid reflux stream is expanded to the feed pressure and fed into the stabilizer column.

## Claims

### Claim 1

A method of producing a stabilized hydrocarbon condensate stream, comprising:
providing a pressurized unstabilized hydrocarbon condensate stream at a first temperature, said first temperature being below a second temperature;
partially evaporating the pressurized unstabilized hydrocarbon condensate stream whereby the pressurized unstabilized hydrocarbon condensate stream becomes a mixed phase pressurized unstabilized hydrocarbon stream at an initial pressure;
expanding the mixed phase pressurized unstabilized hydrocarbon stream from said initial pressure to a feed pressure;
providing the mixed phase pressurized unstabilized hydrocarbon stream at said feed pressure to a stabilizer column at a first inlet location;
discharging from a bottom end of the stabilizer column a liquid phase comprising stabilized hydrocarbon condensate, wherein a first vapour/liquid contacting device configured to allow contact of the vapour and liquid in the stabilizer column is located between the bottom end of the stabilizer column and the first inlet location;
discharging from a top end of the stabilizer column a vapour phase;
compressing the vapour phase being discharged from the top end of the stabilizer column to an auxiliary pressure, thereby forming a compressed overhead vapour stream, whereby the auxiliary pressure is higher than the feed pressure;
passing the compressed overhead vapour stream through a heat exchanger;
passing a coolant stream having a temperature lower than the temperature of the compressed overhead vapour stream through the heat exchanger in indirect heat exchanging contact with the compressed overhead vapour stream, whereby heat from the compressed overhead vapour stream is passed to the coolant stream, wherein the compressed overhead vapour stream becomes a partially condensed overhead stream at said second temperature;
passing the partially condensed overhead stream into an overhead separator and in the overhead separator separating the partially condensed overhead stream into a vapour effluent stream and a liquid stream;
discharging the vapour effluent stream from the overhead separator;
discharging the liquid stream from the overhead separator;
dividing the overhead liquid stream being discharged from the overhead separator at said second temperature into a liquid reflux stream and a liquid effluent stream;
expanding the liquid reflux stream to the feed pressure;
providing the liquid reflux stream at said feed pressure to the stabilizer column at a second inlet location, said second inlet location being at a level gravitationally above the first inlet location, wherein a second vapour/liquid contacting device configured to allow contact of the vapour and liquid in the stabilizer column is located between the first inlet location and the second inlet location;
contacting the liquid reflux stream with a vapour part of the mixed phase pressurized unstabilized hydrocarbon stream in the second vapour/liquid contacting device within the stabilizer column.

### Claim 2 (depends on 1)

The method of claim 1, wherein pressurized unstabilized hydrocarbon condensate stream comprises at least condensed C5+ components, methane, whereby the amount of methane is in the range of from 50 mol % to 80 mol % of the pressurized unstabilized hydrocarbon condensate stream.

### Claim 3 (depends on 1)

The method of claim 1, wherein said partially evaporating the pressurized unstabilized hydrocarbon condensate stream comprises indirectly heat exchanging the pressurized unstabilized hydrocarbon condensate stream in a feed-effluent heat exchanger against an effluent stream being fed to the feed-effluent heat exchanger at the second temperature, wherein the effluent stream at said second temperature consists of one or both of the vapour effluent stream and the liquid effluent stream.

### Claim 4 (depends on 3)

The method of claim 3, wherein the effluent stream at said second temperature comprises the liquid effluent stream, said method further comprising:
passing the liquid effluent stream to the feed-effluent heat exchanger.

### Claim 5 (depends on 1)

The method of claim 1, wherein the first temperature is below the temperature of said coolant stream and the second temperature is above the temperature of said coolant stream.

### Claim 6 (depends on 1)

The method of claim 1, further comprising adding heat from a heat source to the bottom end of the stabilizer column below the first vapour/liquid contacting device.

### Claim 7 (depends on 1)

The method of claim 1, wherein said expanding the mixed phase pressurized unstabilized hydrocarbon stream from said initial pressure to a feed pressure and said providing of the mixed phase pressurized unstabilized hydrocarbon stream to the stabilizer column both comprise:
passing the mixed phase pressurized unstabilized hydrocarbon stream into an inlet separator;
separating the mixed phase pressurized unstabilized hydrocarbon stream into a pressurized liquid hydrocarbon feed stream and a pressurized vapour hydrocarbon feed stream;
discharging the pressurized vapour hydrocarbon feed stream from the inlet separator;
passing the pressurized vapour hydrocarbon feed stream being discharged from the inlet separator into the stabilizer column at the first inlet location;
discharging the pressurized liquid hydrocarbon feed stream from the inlet separator;
passing the pressurized liquid hydrocarbon feed stream being discharged from the inlet separator into the stabilizer column at a third location located gravitationally below the first inlet location and above the first vapour/liquid contacting device.

### Claim 8 (depends on 7)

The method of claim 7, wherein said passing of said mixed phase pressurized unstabilized hydrocarbon stream into the inlet separator comprises lowering the pressure from the initial pressure to an intermediate pressure which is lower than the initial pressure and higher than the feed pressure, and further carrying out said separating of the mixed phase pressurized unstabilized hydrocarbon stream in the inlet separator at said intermediate pressure.

### Claim 9 (depends on 7)

The method of claim 7, further comprising the steps of:
cooling the liquid phase comprising the stabilized hydrocarbon condensate being discharged from the bottom end of the stabilizer column whereby discharging heat from the liquid phase thereby becoming a cooled stream comprising the stabilized hydrocarbon condensate;
splitting the cooled stream comprising the stabilized hydrocarbon condensate into a recycle stream and a discharge stream;
passing the discharge stream to a condensate storage tank;
pumping the recycle stream up to above the first vapour/liquid contacting device and below the first inlet location; and
feeding the recycle stream back into the stabilizer column at a level above the first vapour/liquid contacting device and below the first inlet location and at a first flow rate of the stabilizer column.

### Claim 10 (depends on 9)

The method of claim 9, further comprising:
determining a second flow rate of the stabilizer column, said second flow rate comprising a flow rate of the pressurized liquid hydrocarbon feed stream being discharged from the inlet separator;
adjusting the first flow rate whereby the sum of the first flow rate and the second flow rate exceeds a pre-determined minimum liquid feed rate into the stabilizer column.

### Claim 11 (depends on 1)

The method of claim 1, wherein said step of compressing the vapour phase being discharged from the top end of the stabilizer column to an auxiliary pressure comprises passing the vapour phase though an overhead compressor system comprising a plurality of overhead compressors, whereby prior to passing the vapour phase dividing the vapour phase being discharged from the top end of the stabilizer column into two or more part streams and passing each of the part streams through one of the overhead compressors whereby at least one overhead compressor is provided per part stream and whereby an equal number of compressed overhead vapour part streams is provided at the auxiliary pressure as there are part streams.

### Claim 12 (depends on 1, 11)

The method of claim 11, wherein each of the compressed overhead vapour part streams are de-superheated by passing each of the compressed overhead vapour part streams through a de-superheater heat exchanger whereby at least one de-superheater heat exchanger is provided per compressed overhead vapour part stream, and then all of the compressed overhead vapour part streams are recombined to form the compressed overhead vapour stream that is passed through the heat exchanger of claim 1.

### Claim 13 (depends on 1)

The method of claim 1, wherein the step of providing the pressurized unstabilized hydrocarbon condensate stream at said first temperature comprises:
providing a pressurized natural gas feed stream, said pressurized natural gas feed stream comprising a component selected from the group consisting of methane, ethane, propane, butanes, C5+ components, one or more volatile inert components, and any combination thereof, whereby at least 80 mol % is methane;
partially condensing said pressurized natural gas feed stream, whereby condensing at least the C5+ components, thereby creating a partially condensed natural gas stream;
passing the partially condensed natural gas stream through a liquids extraction device and extracting the pressurized unstabilized hydrocarbon condensate stream from the refrigerated natural gas stream, said pressurized unstabilized hydrocarbon condensate stream comprising at least the condensed C5+ components.

### Claim 14 (depends on 13)

The method of claim 13, further comprising
discharging a lean natural gas stream from the liquids extraction device simultaneously with the pressurized unstabilized hydrocarbon condensate stream,
further refrigerating the lean natural gas stream for fully condensing the lean natural gas stream, and
subsequently depressurizing the lean natural gas stream to produce a flash vapour stream and a liquefied natural gas stream.

### Claim 15 (depends on 14)

The method of claim 14, wherein said partially evaporating the pressurized unstabilized hydrocarbon condensate stream comprises indirectly heat exchanging the pressurized unstabilized hydrocarbon condensate stream in a feed-effluent heat exchanger against an effluent stream being fed to the feed-effluent heat exchanger at the second temperature, wherein the effluent stream at said second temperature consists of one or both of the vapour effluent stream and the liquid effluent stream and wherein the effluent stream being discharged from the feed-effluent heat exchanger is recombined with the lean natural gas stream, prior to said further refrigerating.

### Claim 16 (depends on 3)

The method of claim 3, wherein the effluent stream at said second temperature comprises the vapour effluent stream.

### Claim 17 (depends on 16)

The method of claim 16 further comprising:
passing the vapour effluent stream being discharged from the overhead separator to the feed-effluent heat exchanger.