CA2552865A1 - Method for selective extraction of natural gas liquids from "rich" natural gas - Google Patents
Method for selective extraction of natural gas liquids from "rich" natural gas Download PDFInfo
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- CA2552865A1 CA2552865A1 CA002552865A CA2552865A CA2552865A1 CA 2552865 A1 CA2552865 A1 CA 2552865A1 CA 002552865 A CA002552865 A CA 002552865A CA 2552865 A CA2552865 A CA 2552865A CA 2552865 A1 CA2552865 A1 CA 2552865A1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
- F25J3/061—Natural gas or substitute natural gas
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/0635—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/064—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/0645—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/067—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of carbon dioxide
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—Nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/50—Oxygen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/80—Carbon dioxide
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/62—Ethane or ethylene
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/64—Propane or propylene
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- 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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Abstract
A method for selective extraction of natural gas liquids from "rich" natural gas. The method involves the step of effecting a heat exchange between a rich natural gas stream and a refrigerant fluid to lower a temperature of the rich natural gas stream. The heat exchange is controlled to lower the temperature of the rich natural gas stream to a selected hydrocarbon dew point in order to condense at least one selected hydrocarbon liquids carried in the rich natural gas stream.
Description
TITLE OF THE INVEN'TION:
Method for selective extraction of natural gas liquids from "rich" natural gas FIELD OF THE INVENTION
The present invention relates to a method for selective extraction of natural gas liquids from "rich" natural gas BACKGROUND OF THE INVENTION
Natural gas coniing from a producing well contains many natural gas liquids (NGLs) that are commonly removed. The removal of natural NGLs usually takes place in a relatively centralized processing plant. The objective is to reduce the hydrocarbon dew point to prevent problerns in the pipelines from liquid fallout. To remove NGLs, there are three common processes; Refrigeration, Lean Oil Absorption and Cryogenic.
With Refrigeration, a refrigeration plant is employed to provide cold to lower the temperature of the natmal gas. Refrigeration is able to extract a large percentage of propane and most of the butane and heavier components.
With Lean Oil Absorption, an absorbing oil with an affinity for NGLs is brought into contact with natural gas in a contact tower where it soaks up a high proportion of NGLs. The "rich" abscirption oil, now containing NGLs exits the absorption tower. This "rich" mixture of absorbing oil and NGLs is chilled to -30 F to separate the NGLs and absorbing oil. This process can extract 90% of the propane and heavier hydrocarbons and about 30% of the ethane.
The cryogenic process enables higher recoveries of ethane. The first generation cryogenic plants were able to extract up to 70% of the ethane from the gas, since the early 1990s, modifications to the cryogenic process have allowed ethane recoveries up to 99%
extraction level. This increase in recovery comes with higher operating costs.
There are a number of different ways to chill the gas the one most commonly used is the turbo expander process. In this process external refrigerants are used to cool the natural gas stream, then an expansion turbine is used to rapidly expand the chilled gases, which causes the temperature to drop significantly. This rapid temperature drop condenses ethane and other hydrocarbons in the gas stream while maintaining methane in a gaseous form.
Operations of gas processing plants in reduced recovery modes is difficult, the plants are typically designed to achieve high recoveries of all the NGLs and are not designed to recover only pentanes and heavier or only butanes.
SUMMARY OF THE INVENTION
There is provided a method for selective extraction of natural gas liquids from "rich"
natural gas. The method involves the step of effecting a heat exchange between a rich natural gas stream and a refrigerant fluid to lower a temperature of the rich natural gas stream. The heat exchange is controlled to lower the temperature of the rich natural gas stream to a selected hydrocarbon dew point in order to condense at least one selected hydrocarbon liquids carried in the rich natural gas stream.
BRIEF DESCRIPTION OF THE DRAWINGS
These and other features of the invention will become more apparent from the following description in which reference is made to the appended drawings, the drawings are for the purpose of illustration only and are not intended to in any way limit the scope of the invention to the particular embodiment or embodiments shown, wherein:
FIG. 1 is a schematic diagram of a facility equipped with indirect cooling in accordance with the teachings of the present invention.
FIG. 2 is a schematic diagram showing a variation of the indirect cooling illustrated in FIG. 1.
DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT
The preferred method will now be described with reference to FIG. 1.
Referring to FIG. 1, "rich" natural gas stream 20 is straddled into stream 30 for indirect pre-cooling in heat exchanger 1. The cooling is provided by the countercurrent flow of stream 40. The now colder stream 31 then enters separator 2 where water and heavy hydrocarbons are condensed and separated from lighter fractions (hydrocarbons, carbon dioxide, nitrogen, etc..). The separated heavier fractions exit separator vessel 2 through line 60. The lighter fractions exit through line 32 which then enters heat exchanger cold box section 6 for further cooling. The colder stream 33 now enters separator vessel 3. The condensed and separated propane exits separator vessel 3 through line 61. The separated lighter fractions leave separator 3 through line 34 for further cooling in heat exchanger cold box section 7. The colder stream 35 now enters separator vessel 4. The condensed and separated carbon dioxide exits separator vessel 4 through line 62. The separated lighter fractions leave separator 6 through line 36 for fw-ther cooling in heat exchanger cold box section 8. The colder stream 37 now enters separator vessel 5. The condensed and separated ethane exits separator vessel 5 through line 63. The now "lean" gas leaves separator 5 through line 38 for pre-heating in cold box section 7 and cold box section 6.
The now warmer "lean" gas exits cold box through stream 39 and mixes with the vaporized LNG
stream 52 to form the mixture streani 40. The mixed "lean" gas now enters heat exchanger 1 for pre-heating, it then exits it at or near transmission line temperature through stream 41. The refrigerant is LNG supplied from tank 9 and pressurized by pump 10 into stream 51. The pressurized LNG flows fnst into heat exchanger cold box section 8 where it begins to pick up heat, then into heat exchanger cold box section section 7 and finally into heat exchanger cold box section 6. This vaporized stream exits the cold box as stream 52 and is mixed with the "lean" gas stream 49 to forrn a "lean" mixture as stream 40.
FIG.2 shows another arrangement for indirect contact method for extraction of natural gas liquids where the cold energy supply fluid is one other than LNG, the main difference being that when LNG is used it can be injected into the transmission pipeline while an optional fluid may or may not be injected into the pipeline. "Rich" natural gas stream 20 is straddled into stream 30 for indirect pre-cooling in heat exchanger 1. The cooling is provided by the countercurrent flow of stream 39. The now colder stream 31 then enters separator 2 where water and heavy hydrocarbons are condensed and separated from lighter fractions (hydrocarbons, carbon dioxide, nitrogen, etc..). The separated heavier fractions exit separator vessel 2 through line 60. The lighter fractions exit through line 32 which then enters heat exchanger cold box section 6 for further cooling. The colder stream 33 now enters separator vessel 3. The condensed and separated propane exits separator vessel 3 through line 61. The separated lighter fractions leave separator 3 through line 34 for further cooling in heat exchanger cold box section 7. The colder stream 35 now enters separator vessel 4. The condensed and separated carbon dioxide exits separator vessel 4 through line 62. The separated lighter fractians leave separator 4 through line 36 for further cooling in heat exchanger cold box section 8. The colder stream 37 now enters separator vessel 5. The condensed and separated ethane exits separator vessel 5 through line 63. The now 'lean" gas leaves separator 5 through line 38 for pre-heating in cold box section 7 and cold box section 6. The now warmer "lean" gas exits cold box through stream 39. The "lean" gas now enters heat exchanger 1 for pre-heating, it then exits it at a near transmission line temperature through stream 40. The refrigerant is supplied from tank 9 into stream 51.
This refrigerant flows first into heat exchanger cold box section 8 where it begins to pick up heat, then into heat exchanger cold box section section 7 and finally into heat exchanger cold box section 6.
This vaporized stream exits the cold box as stream 52. For those skilled in the art, the number of heat exchangers and separators can be re-arranged to achieve the desired separation of hydrocarbons and other components present in the "rich" gas stream.
Liquid Natural Gas (LNG) has been selected for the purpose of illustration. It will be appreciated that other refrigerants such as liquid nitrogen, liquid carbon dioxide, liquid oxygen and the like can be used to condense the "rich" gas stream. It is preferred that the refrigerant fluid be within the cryogenic temperature range, merely because colder temperatures are required in order to condense some of the natural gas liquids, such as ethane.
Other hydrocarbon refrigerants can be used such as ethane and propane. For example, liquid carbon dioxide could be used as a refrigerant to condense a number of natural gas liquids, but would not be effective in condensing ethane. There are drawbacks to the use of some refrigerant fluids, such as liquid oxygen. Liquid oxygen could be used, but is not preferred due to safety concerns. Liquid Natural Gas and Liquid Nitrogen are two of the more viable refrigerants which could be used.
In the preferred method, refrigerant fluids provide the "cold energy" required to condense and extract the NGLs . A typical straddle plant is designed to achieve high recoveries of all NGLs and the "turndown" to lower recoveries are difficult to obtain. The above method allows for ease of "turndown" by simply changing the temperature set point controller which then changes the LNG flow rate. As the LNG gives up its cold energy to condense the NGLs in the "rich" stream it becomes a "lean" gas ready for distribution.
Existing plants operate in a mode that recovers at least some percentage of all components, it is not generally possible to operate the plants to achieve a specific 5 hydrocarbon dew point. Control of hydrocarbon dew point for gas transportation is critical due to the influence of ambient temperatures and pressure reductions during transportation that can cause liquid fallout. To reach higher extraction levels more expensive metallurgy, more compression, and more capital investment is required.
According to the present invention there is provided a method for liquefaction and extraction of NGLs from natural gas. A pre-cooling takes place in a heat exchanger of the incoming "rich" natural gas streain, containing methane, ethane, propane, butanes, pentanes, other heavier hydrocarbons, water and carbon dioxide with a countercurrent flow of "lean" natural gas. Separation of water and heavier hydrocarbons from lighter hydrocarbons then takes place in a series of separators by controlling the temperature at each separator through a heat exchange with refrigerant fluids. Cooling upstream of each separator through a heat exchange with refrigerant fluids peimits selective control of the extraction of NGL's.
The method provides for ease of "turndown" to achieve high or low recoveries ratios between and Hydrocarbon Dew Point (HDC) control. The use of the above described method at a straddle plant facility provides a distinct advantage over methods currently in use.
Existing systems bring the pressure of the natural gas down to remove the natural gas liquids and then increasing the pressure of the natural gas back up in order to return the natural gas to the pipeline after processing. With the present method, the natural gas can be freed of the natural gas liquids without a change in pressure.
In this patent dxument, the word "comprising" is used in its non-limiting sense to mean that items following the word are included, but items not specifically mentioned are not excluded. A reference to an element by the indefinite article "a" does not exclude the possibility that more than one of the element is present, unless the context clearly requires that there be one and only one of the elements.
It will be apparent to one skilled in the art that modifications may be made to the illustrated embodiment without departing from the spirit and scope of the invention as hereinafter defined in the Claims.
Method for selective extraction of natural gas liquids from "rich" natural gas FIELD OF THE INVENTION
The present invention relates to a method for selective extraction of natural gas liquids from "rich" natural gas BACKGROUND OF THE INVENTION
Natural gas coniing from a producing well contains many natural gas liquids (NGLs) that are commonly removed. The removal of natural NGLs usually takes place in a relatively centralized processing plant. The objective is to reduce the hydrocarbon dew point to prevent problerns in the pipelines from liquid fallout. To remove NGLs, there are three common processes; Refrigeration, Lean Oil Absorption and Cryogenic.
With Refrigeration, a refrigeration plant is employed to provide cold to lower the temperature of the natmal gas. Refrigeration is able to extract a large percentage of propane and most of the butane and heavier components.
With Lean Oil Absorption, an absorbing oil with an affinity for NGLs is brought into contact with natural gas in a contact tower where it soaks up a high proportion of NGLs. The "rich" abscirption oil, now containing NGLs exits the absorption tower. This "rich" mixture of absorbing oil and NGLs is chilled to -30 F to separate the NGLs and absorbing oil. This process can extract 90% of the propane and heavier hydrocarbons and about 30% of the ethane.
The cryogenic process enables higher recoveries of ethane. The first generation cryogenic plants were able to extract up to 70% of the ethane from the gas, since the early 1990s, modifications to the cryogenic process have allowed ethane recoveries up to 99%
extraction level. This increase in recovery comes with higher operating costs.
There are a number of different ways to chill the gas the one most commonly used is the turbo expander process. In this process external refrigerants are used to cool the natural gas stream, then an expansion turbine is used to rapidly expand the chilled gases, which causes the temperature to drop significantly. This rapid temperature drop condenses ethane and other hydrocarbons in the gas stream while maintaining methane in a gaseous form.
Operations of gas processing plants in reduced recovery modes is difficult, the plants are typically designed to achieve high recoveries of all the NGLs and are not designed to recover only pentanes and heavier or only butanes.
SUMMARY OF THE INVENTION
There is provided a method for selective extraction of natural gas liquids from "rich"
natural gas. The method involves the step of effecting a heat exchange between a rich natural gas stream and a refrigerant fluid to lower a temperature of the rich natural gas stream. The heat exchange is controlled to lower the temperature of the rich natural gas stream to a selected hydrocarbon dew point in order to condense at least one selected hydrocarbon liquids carried in the rich natural gas stream.
BRIEF DESCRIPTION OF THE DRAWINGS
These and other features of the invention will become more apparent from the following description in which reference is made to the appended drawings, the drawings are for the purpose of illustration only and are not intended to in any way limit the scope of the invention to the particular embodiment or embodiments shown, wherein:
FIG. 1 is a schematic diagram of a facility equipped with indirect cooling in accordance with the teachings of the present invention.
FIG. 2 is a schematic diagram showing a variation of the indirect cooling illustrated in FIG. 1.
DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT
The preferred method will now be described with reference to FIG. 1.
Referring to FIG. 1, "rich" natural gas stream 20 is straddled into stream 30 for indirect pre-cooling in heat exchanger 1. The cooling is provided by the countercurrent flow of stream 40. The now colder stream 31 then enters separator 2 where water and heavy hydrocarbons are condensed and separated from lighter fractions (hydrocarbons, carbon dioxide, nitrogen, etc..). The separated heavier fractions exit separator vessel 2 through line 60. The lighter fractions exit through line 32 which then enters heat exchanger cold box section 6 for further cooling. The colder stream 33 now enters separator vessel 3. The condensed and separated propane exits separator vessel 3 through line 61. The separated lighter fractions leave separator 3 through line 34 for further cooling in heat exchanger cold box section 7. The colder stream 35 now enters separator vessel 4. The condensed and separated carbon dioxide exits separator vessel 4 through line 62. The separated lighter fractions leave separator 6 through line 36 for fw-ther cooling in heat exchanger cold box section 8. The colder stream 37 now enters separator vessel 5. The condensed and separated ethane exits separator vessel 5 through line 63. The now "lean" gas leaves separator 5 through line 38 for pre-heating in cold box section 7 and cold box section 6.
The now warmer "lean" gas exits cold box through stream 39 and mixes with the vaporized LNG
stream 52 to form the mixture streani 40. The mixed "lean" gas now enters heat exchanger 1 for pre-heating, it then exits it at or near transmission line temperature through stream 41. The refrigerant is LNG supplied from tank 9 and pressurized by pump 10 into stream 51. The pressurized LNG flows fnst into heat exchanger cold box section 8 where it begins to pick up heat, then into heat exchanger cold box section section 7 and finally into heat exchanger cold box section 6. This vaporized stream exits the cold box as stream 52 and is mixed with the "lean" gas stream 49 to forrn a "lean" mixture as stream 40.
FIG.2 shows another arrangement for indirect contact method for extraction of natural gas liquids where the cold energy supply fluid is one other than LNG, the main difference being that when LNG is used it can be injected into the transmission pipeline while an optional fluid may or may not be injected into the pipeline. "Rich" natural gas stream 20 is straddled into stream 30 for indirect pre-cooling in heat exchanger 1. The cooling is provided by the countercurrent flow of stream 39. The now colder stream 31 then enters separator 2 where water and heavy hydrocarbons are condensed and separated from lighter fractions (hydrocarbons, carbon dioxide, nitrogen, etc..). The separated heavier fractions exit separator vessel 2 through line 60. The lighter fractions exit through line 32 which then enters heat exchanger cold box section 6 for further cooling. The colder stream 33 now enters separator vessel 3. The condensed and separated propane exits separator vessel 3 through line 61. The separated lighter fractions leave separator 3 through line 34 for further cooling in heat exchanger cold box section 7. The colder stream 35 now enters separator vessel 4. The condensed and separated carbon dioxide exits separator vessel 4 through line 62. The separated lighter fractians leave separator 4 through line 36 for further cooling in heat exchanger cold box section 8. The colder stream 37 now enters separator vessel 5. The condensed and separated ethane exits separator vessel 5 through line 63. The now 'lean" gas leaves separator 5 through line 38 for pre-heating in cold box section 7 and cold box section 6. The now warmer "lean" gas exits cold box through stream 39. The "lean" gas now enters heat exchanger 1 for pre-heating, it then exits it at a near transmission line temperature through stream 40. The refrigerant is supplied from tank 9 into stream 51.
This refrigerant flows first into heat exchanger cold box section 8 where it begins to pick up heat, then into heat exchanger cold box section section 7 and finally into heat exchanger cold box section 6.
This vaporized stream exits the cold box as stream 52. For those skilled in the art, the number of heat exchangers and separators can be re-arranged to achieve the desired separation of hydrocarbons and other components present in the "rich" gas stream.
Liquid Natural Gas (LNG) has been selected for the purpose of illustration. It will be appreciated that other refrigerants such as liquid nitrogen, liquid carbon dioxide, liquid oxygen and the like can be used to condense the "rich" gas stream. It is preferred that the refrigerant fluid be within the cryogenic temperature range, merely because colder temperatures are required in order to condense some of the natural gas liquids, such as ethane.
Other hydrocarbon refrigerants can be used such as ethane and propane. For example, liquid carbon dioxide could be used as a refrigerant to condense a number of natural gas liquids, but would not be effective in condensing ethane. There are drawbacks to the use of some refrigerant fluids, such as liquid oxygen. Liquid oxygen could be used, but is not preferred due to safety concerns. Liquid Natural Gas and Liquid Nitrogen are two of the more viable refrigerants which could be used.
In the preferred method, refrigerant fluids provide the "cold energy" required to condense and extract the NGLs . A typical straddle plant is designed to achieve high recoveries of all NGLs and the "turndown" to lower recoveries are difficult to obtain. The above method allows for ease of "turndown" by simply changing the temperature set point controller which then changes the LNG flow rate. As the LNG gives up its cold energy to condense the NGLs in the "rich" stream it becomes a "lean" gas ready for distribution.
Existing plants operate in a mode that recovers at least some percentage of all components, it is not generally possible to operate the plants to achieve a specific 5 hydrocarbon dew point. Control of hydrocarbon dew point for gas transportation is critical due to the influence of ambient temperatures and pressure reductions during transportation that can cause liquid fallout. To reach higher extraction levels more expensive metallurgy, more compression, and more capital investment is required.
According to the present invention there is provided a method for liquefaction and extraction of NGLs from natural gas. A pre-cooling takes place in a heat exchanger of the incoming "rich" natural gas streain, containing methane, ethane, propane, butanes, pentanes, other heavier hydrocarbons, water and carbon dioxide with a countercurrent flow of "lean" natural gas. Separation of water and heavier hydrocarbons from lighter hydrocarbons then takes place in a series of separators by controlling the temperature at each separator through a heat exchange with refrigerant fluids. Cooling upstream of each separator through a heat exchange with refrigerant fluids peimits selective control of the extraction of NGL's.
The method provides for ease of "turndown" to achieve high or low recoveries ratios between and Hydrocarbon Dew Point (HDC) control. The use of the above described method at a straddle plant facility provides a distinct advantage over methods currently in use.
Existing systems bring the pressure of the natural gas down to remove the natural gas liquids and then increasing the pressure of the natural gas back up in order to return the natural gas to the pipeline after processing. With the present method, the natural gas can be freed of the natural gas liquids without a change in pressure.
In this patent dxument, the word "comprising" is used in its non-limiting sense to mean that items following the word are included, but items not specifically mentioned are not excluded. A reference to an element by the indefinite article "a" does not exclude the possibility that more than one of the element is present, unless the context clearly requires that there be one and only one of the elements.
It will be apparent to one skilled in the art that modifications may be made to the illustrated embodiment without departing from the spirit and scope of the invention as hereinafter defined in the Claims.
Claims (8)
1. A method for selective extraction of natural gas liquids from "rich"
natural gas, comprising the step of:
effecting a heat exchange between a rich natural gas stream and a refrigerant fluid to lower a temperature of the rich natural gas stream, the heat exchange being controlled to lower the temperature of the rich natural gas stream to a selected hydrocarbon dew point in order to condense at least one selected hydrocarbon liquids carried in the rich natural gas stream.
natural gas, comprising the step of:
effecting a heat exchange between a rich natural gas stream and a refrigerant fluid to lower a temperature of the rich natural gas stream, the heat exchange being controlled to lower the temperature of the rich natural gas stream to a selected hydrocarbon dew point in order to condense at least one selected hydrocarbon liquids carried in the rich natural gas stream.
2. The method as defined in Claim 1, wherein the refrigerant fluid is one of Liquid Natural Gas (LNG), Liquid Nitrogen, Liquid Oxygen, or Liquid Carbon Dioxide.
3. The method as defined in Claim 1, wherein the refrigerant fluid is at a starting temperature which is within a cryogenic range.
4. The method as defined in Claim 1, wherein a series of heat exchanges are effected sequentially at different temperatures to achieve a different selected hydrocarbon dew point at each heat exchange in order to condense different selected hydrocarbon liquids with each heat exchange.
5. A method for selective extraction of natural gas liquids from "rich"
natural gas, comprising the step of:
effecting a series of heat exchanges between a rich natural gas stream and a refrigerant fluid in a cryogenic temperature range selected from one of Liquid Natural Gas (LNG) or Liquid Nitrogen to lower the temperature of the rich natural gas stream, each heat exchange being adapted to lower the temperature of the rich natural gas stream to a different selected hydrocarbon dew point in order to condense a different hydrocarbon liquid carried in the rich natural gas stream.
natural gas, comprising the step of:
effecting a series of heat exchanges between a rich natural gas stream and a refrigerant fluid in a cryogenic temperature range selected from one of Liquid Natural Gas (LNG) or Liquid Nitrogen to lower the temperature of the rich natural gas stream, each heat exchange being adapted to lower the temperature of the rich natural gas stream to a different selected hydrocarbon dew point in order to condense a different hydrocarbon liquid carried in the rich natural gas stream.
6. A straddle plant, comprising:
a storage vessel for a refrigerant fluid;
a separator adapted to separate natural gas liquids (NGL) from rich natural gas;
a heat exchanger having a refrigerant flow path supplied by the storage vessel and a rich natural gas flow path connected to an inlet of the separator, the heat exchanger being adapted to lower a temperature of a rich natural gas stream entering the separator to a selected hydrocarbon dew point in order to condense at least one hydrocarbon liquid carried in the rich natural gas stream, the temperature of the rich natural gas stream being controlled by circulation of refrigerant through the heat exchanger.
a storage vessel for a refrigerant fluid;
a separator adapted to separate natural gas liquids (NGL) from rich natural gas;
a heat exchanger having a refrigerant flow path supplied by the storage vessel and a rich natural gas flow path connected to an inlet of the separator, the heat exchanger being adapted to lower a temperature of a rich natural gas stream entering the separator to a selected hydrocarbon dew point in order to condense at least one hydrocarbon liquid carried in the rich natural gas stream, the temperature of the rich natural gas stream being controlled by circulation of refrigerant through the heat exchanger.
7. The straddle plant as defined in Claim 6, wherein there is more than one separator, each separator operating at a different selected hydrocarbon dew point in order to condense different hydrocarbon liquids carried in the rich natural gas stream.
8. The straddle plant as defined in Claim 6, wherein the refrigerant fluid is one of Liquid Natural Gas (LNG), Liquid Nitrogen, Liquid Oxygen, or Liquid Carbon Dioxide.
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| CA2552865A CA2552865C (en) | 2006-07-14 | 2006-07-14 | Method for selective extraction of natural gas liquids from "rich" natural gas |
| PCT/CA2007/001247 WO2008006221A1 (en) | 2006-07-14 | 2007-07-13 | Method for selective extraction of natural gas liquids from 'rich' natural gas |
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| CA2552865A CA2552865C (en) | 2006-07-14 | 2006-07-14 | Method for selective extraction of natural gas liquids from "rich" natural gas |
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| FR2950686B1 (en) * | 2009-09-29 | 2012-02-17 | Technip France | PROCESS FOR TREATING A GASEOUS EFFLUENT AND ASSOCIATED PROCESSING PLANT. |
| US20130149382A1 (en) * | 2010-05-27 | 2013-06-13 | Exosect Limited | Liquid compositions comprising a sustained release system for insecticides |
| CA2790961C (en) | 2012-05-11 | 2019-09-03 | Jose Lourenco | A method to recover lpg and condensates from refineries fuel gas streams. |
| CA2798057C (en) | 2012-12-04 | 2019-11-26 | Mackenzie Millar | A method to produce lng at gas pressure letdown stations in natural gas transmission pipeline systems |
| CA2813260C (en) | 2013-04-15 | 2021-07-06 | Mackenzie Millar | A method to produce lng |
| CA2958091C (en) | 2014-08-15 | 2021-05-18 | 1304338 Alberta Ltd. | A method of removing carbon dioxide during liquid natural gas production from natural gas at gas pressure letdown stations |
| WO2017045055A1 (en) | 2015-09-16 | 2017-03-23 | 1304342 Alberta Ltd. | A method of preparing natural gas at a gas pressure reduction stations to produce liquid natural gas (lng) |
| WO2019095031A1 (en) | 2017-11-14 | 2019-05-23 | 1304338 Alberta Ltd. | A method to recover and process methane and condensates from flare gas systems |
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| US3754405A (en) * | 1969-02-10 | 1973-08-28 | Black Sivalls & Bryson Inc | Method of controlling the hydrocarbon dew point of a gas stream |
| US4430103A (en) * | 1982-02-24 | 1984-02-07 | Phillips Petroleum Company | Cryogenic recovery of LPG from natural gas |
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| CA2552865C (en) | 2016-05-10 |
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