CA2805272C - Methods and systems for recovering liquified petroleum gas from natural gas - Google Patents
Methods and systems for recovering liquified petroleum gas from natural gas Download PDFInfo
- Publication number
- CA2805272C CA2805272C CA2805272A CA2805272A CA2805272C CA 2805272 C CA2805272 C CA 2805272C CA 2805272 A CA2805272 A CA 2805272A CA 2805272 A CA2805272 A CA 2805272A CA 2805272 C CA2805272 C CA 2805272C
- Authority
- CA
- Canada
- Prior art keywords
- stream
- gas stream
- fractionation column
- deethanizer
- component
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 238000000034 method Methods 0.000 title claims abstract description 48
- 239000003345 natural gas Substances 0.000 title description 9
- 239000003209 petroleum derivative Substances 0.000 title description 2
- 238000005194 fractionation Methods 0.000 claims abstract description 143
- 239000007788 liquid Substances 0.000 claims abstract description 62
- 238000010992 reflux Methods 0.000 claims description 39
- 238000001816 cooling Methods 0.000 claims description 17
- 238000000926 separation method Methods 0.000 claims description 11
- 238000011144 upstream manufacturing Methods 0.000 claims 2
- 238000011084 recovery Methods 0.000 abstract description 4
- 239000013589 supplement Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 113
- 239000000306 component Substances 0.000 description 83
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 10
- 239000001257 hydrogen Substances 0.000 description 7
- 229910052739 hydrogen Inorganic materials 0.000 description 7
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 6
- 239000006096 absorbing agent Substances 0.000 description 6
- 238000012545 processing Methods 0.000 description 6
- 239000001294 propane Substances 0.000 description 5
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 4
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 238000004821 distillation Methods 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000003507 refrigerant Substances 0.000 description 4
- 239000003915 liquefied petroleum gas Substances 0.000 description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 3
- 238000005057 refrigeration Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 238000004088 simulation Methods 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 239000001273 butane Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Classifications
-
- 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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
-
- 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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
-
- 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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
-
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
- F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
-
- 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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
-
- 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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
-
- 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
-
- 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
- F25J2270/12—External refrigeration with liquid vaporising loop
-
- 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
- F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
Abstract
A process and system is provided for separating a feed gas stream containing methane, at least one C2 component, at least one C3 component, and optionally heavier components, into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 and heavier components. The feed stream is cooled, at least partially condensed, and fed to a fractionation column wherein the feed stream is separated into an overhead vapor stream comprising primarily the lighter components of the feed stream and a bottoms liquid stream comprising primarily the heavier components of the feed stream. The introduction of a reboiler onto the fractionation column assists in removing co-absorbed C2 and lighter components from the fractionation column bottoms thereby facilitating more efficient operation of a downstream deethanizer column. Addition of residue recycle can further supplement recovery of desired components.
Description
, , METHODS AND SYSTEMS FOR RECOVERING LIQUIFIED
PETROLEUM GAS FROM NATURAL GAS
RELATED APPLICATION
This application claims the benefit of U.S. Provisional Patent Application No.
61/360,753, filed July 1, 2010.
BACKGROUND OF THE INVENTION
Field of the Invention The present invention is directed toward processes and systems for recovering liquefied petroleum gas (LPG) from a hydrocarbon gas stream, especially a natural gas stream or a refinery gas stream. Particularly, the processes and systems described herein may be utilized to enhance LPG recovery, particularly when processing higher pressure or leaner feed streams thereby providing broader applicability compared to previous processes.
Description of the Prior Art Natural gas comprises primarily methane, but can also include varying amounts of heavy hydrocarbon components such as ethane, propane, butane, and pentane, for example.
It is well known that natural gas streams can be separated into their respective component parts. Such processes involve a combination of chilling, expansion, distillation and/or like operations to separate methane and ethane from C3 and heavier hydrocarbon components.
Typically the separation made is of methane and ethane from propane and heavier compo-nents. If economically desirable, the ethane could also be recovered and similarly, it is desirable in many instances to further fractionate the recovered C3 (or alternatively C2) and heavier components.
One process that has been devised for separating a natural gas stream into light and heavy component streams is shown in U.S. Pat. No. 5,771,712. The '712 Patent demon-strates a typical process wherein an overhead stream from a deethanizer is passed into heat exchange with an exit stream from an absorber to cool the overhead stream from the deethanizer to a temperature at which it is partially liquefied. This partially liquefied stream is then introduced into the absorber wherein the liquid portion of the stream passes down-wardly through the absorber to contact a gaseous
PETROLEUM GAS FROM NATURAL GAS
RELATED APPLICATION
This application claims the benefit of U.S. Provisional Patent Application No.
61/360,753, filed July 1, 2010.
BACKGROUND OF THE INVENTION
Field of the Invention The present invention is directed toward processes and systems for recovering liquefied petroleum gas (LPG) from a hydrocarbon gas stream, especially a natural gas stream or a refinery gas stream. Particularly, the processes and systems described herein may be utilized to enhance LPG recovery, particularly when processing higher pressure or leaner feed streams thereby providing broader applicability compared to previous processes.
Description of the Prior Art Natural gas comprises primarily methane, but can also include varying amounts of heavy hydrocarbon components such as ethane, propane, butane, and pentane, for example.
It is well known that natural gas streams can be separated into their respective component parts. Such processes involve a combination of chilling, expansion, distillation and/or like operations to separate methane and ethane from C3 and heavier hydrocarbon components.
Typically the separation made is of methane and ethane from propane and heavier compo-nents. If economically desirable, the ethane could also be recovered and similarly, it is desirable in many instances to further fractionate the recovered C3 (or alternatively C2) and heavier components.
One process that has been devised for separating a natural gas stream into light and heavy component streams is shown in U.S. Pat. No. 5,771,712. The '712 Patent demon-strates a typical process wherein an overhead stream from a deethanizer is passed into heat exchange with an exit stream from an absorber to cool the overhead stream from the deethanizer to a temperature at which it is partially liquefied. This partially liquefied stream is then introduced into the absorber wherein the liquid portion of the stream passes down-wardly through the absorber to contact a gaseous
-2-stream passing upwardly through the absorber. While this processing system has been effective to separate C2 and lighter components from C3 and heavier components, it is relatively inefficient when processing lower pressure feed gas streams. It is also relatively inefficient when processing rich feed gas streams with respect to their C3 and heavier content.
It is particularly ineffective when large amounts of very light gases, such as hydrogen, may be present in the feed gas stream charged to the process. Hydrogen in gaseous streams recovered from refinery operations, which may be desirably separated in such processes, is not uncommon. While the occurrence of hydrogen in significant quantities in natural gas is rare, the presence of hydrogen in similar streams from refinery operations is common.
U.S. Patent No. 6,405,561 discloses a process for recovering C3 and heavier compo-nents from low-pressure natural gas or refinery gas streams. The '561 patent teaches the improvement of cooling and partially condensing a deethanizer overhead gas stream to produce a deethanizer liquid stream that is further cooled and directed into an upper portion of a separator/absorber, which separates the inlet feed stream into a liquid bottoms stream comprising primarily C3 and heavier components and an overhead gas stream comprising primarily C2 and lighter components. The process of the '561 patent is particularly effective for treatment of feed gas streams at lower pressure that contain substantial amounts of very light components, including hydrogen that is often found in refinery applications.
The process of the '561 patent is also effective for treatment of feed gas streams rich with respect to recoverable C3 and heavier components.
However, as feed gas pressure increases, or if feed gas streams with higher quantities of C2 and lighter components are used, the process of the '561 patent becomes less effective due to co-adsorption of these lighter components in the separator/absorber bottoms stream.
As a result, these lighter components tend to reduce the temperature required to partially condense the deethanizer overhead gas stream. Thus, the refrigerant medium used in this condensation operation must be changed from propane to a colder, more horsepow-er-intensive refrigeration media. As a result, the investment in equipment and operating cost is increased substantially.
SUMMARY OF THE INVENTION
In one embodiment of the present invention, there is provided a process for separating a feed gas stream containing methane, at least one C2 component, and at least one C3
It is particularly ineffective when large amounts of very light gases, such as hydrogen, may be present in the feed gas stream charged to the process. Hydrogen in gaseous streams recovered from refinery operations, which may be desirably separated in such processes, is not uncommon. While the occurrence of hydrogen in significant quantities in natural gas is rare, the presence of hydrogen in similar streams from refinery operations is common.
U.S. Patent No. 6,405,561 discloses a process for recovering C3 and heavier compo-nents from low-pressure natural gas or refinery gas streams. The '561 patent teaches the improvement of cooling and partially condensing a deethanizer overhead gas stream to produce a deethanizer liquid stream that is further cooled and directed into an upper portion of a separator/absorber, which separates the inlet feed stream into a liquid bottoms stream comprising primarily C3 and heavier components and an overhead gas stream comprising primarily C2 and lighter components. The process of the '561 patent is particularly effective for treatment of feed gas streams at lower pressure that contain substantial amounts of very light components, including hydrogen that is often found in refinery applications.
The process of the '561 patent is also effective for treatment of feed gas streams rich with respect to recoverable C3 and heavier components.
However, as feed gas pressure increases, or if feed gas streams with higher quantities of C2 and lighter components are used, the process of the '561 patent becomes less effective due to co-adsorption of these lighter components in the separator/absorber bottoms stream.
As a result, these lighter components tend to reduce the temperature required to partially condense the deethanizer overhead gas stream. Thus, the refrigerant medium used in this condensation operation must be changed from propane to a colder, more horsepow-er-intensive refrigeration media. As a result, the investment in equipment and operating cost is increased substantially.
SUMMARY OF THE INVENTION
In one embodiment of the present invention, there is provided a process for separating a feed gas stream containing methane, at least one C2 component, and at least one C3
-3-component into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 component. The process comprises first cooling the feed gas stream to a temperature sufficient to condense the majority of the at least one C3 component in the feed gas stream to produce a cooled feed stream. The cooled feed stream is introduced into a separator vessel to separate the cooled feed stream into a separator gas stream and a separator liquid stream. At least a portion of both of the separator gas and liquid streams from the separator vessel is introduced into a fractionation column to produce a fractionation column bottoms product and a fractionation column overhead residue gas stream. The fractionation column bottoms product is introduced into a deethanizer tower which produces a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream.
In another embodiment of the present invention, there is provided a process for separating a feed gas stream containing methane, at least one C2 component, and at least one C3 component into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 component. The process comprises cooling the feed gas stream to a temperature sufficient to condense the majority of the at least one C3 component therein to produce a cooled feed stream. The cooled feed stream is passed to a fractionation column to produce a liquid fractionation column bottoms product and a fractionation column overhead residue gas stream. The fractionation column including a rcboiler operable to vaporize at least a portion of the fractionation column liquid which is taken from the bottom or near the bottom of the column. The vaporized portion is then reintroduced into the fractionation column. The fractionation column bottoms product is introduced into a deethanizer tower which produces a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream. The deethanizer overhead gas stream is cooled and at least partially condensed thereby producing a deethanizer liquid reflux stream and a deethanizer residue gas stream. Optionally, the deethanizer residue gas stream is combined with at least a portion of the overhead residue gas stream to form a combined residue gas stream. At least a portion of the combined residue gas stream is compressed and cooled to produce a residue gas reflux stream. The residue gas reflux stream is introduced into the fractionation column.
In another embodiment of the present invention, there is provided a process for separating a feed gas stream containing methane, at least one C2 component, and at least one C3 component into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 component. The process comprises cooling the feed gas stream to a temperature sufficient to condense the majority of the at least one C3 component therein to produce a cooled feed stream. The cooled feed stream is passed to a fractionation column to produce a liquid fractionation column bottoms product and a fractionation column overhead residue gas stream. The fractionation column including a rcboiler operable to vaporize at least a portion of the fractionation column liquid which is taken from the bottom or near the bottom of the column. The vaporized portion is then reintroduced into the fractionation column. The fractionation column bottoms product is introduced into a deethanizer tower which produces a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream. The deethanizer overhead gas stream is cooled and at least partially condensed thereby producing a deethanizer liquid reflux stream and a deethanizer residue gas stream. Optionally, the deethanizer residue gas stream is combined with at least a portion of the overhead residue gas stream to form a combined residue gas stream. At least a portion of the combined residue gas stream is compressed and cooled to produce a residue gas reflux stream. The residue gas reflux stream is introduced into the fractionation column.
-4-In a further embodiment of the present invention, there is provided a process for sepa-rating a feed gas stream containing methane, at least one C2 component, and at least one C3 component into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 component. The process comprises cooling the feed gas stream to a temperature sufficient to condense the majority of the at least one C3 component in the feed gas stream to produce a cooled feed stream. The cooled feed stream is passed to a fractionation column to produce a liquid fractionation column bottoms product and a fractionation column overhead residue gas stream. The fractionation column bottoms product is introduced into a deethanizer tower, which produces a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream. -Fhe deethanizer overhead gas stream is cooled and at least partially condensed thereby producing a deethanizer liquid reflux stream and a deethanizer residue gas stream. At least a portion of the fractionation column overhead residue gas stream is compressed and cooled to produce a residue gas reflux stream. The residue gas reflux stream is then introduced into the fractionation column.
In yet another embodiment of the present invention, there is provided a system for separating a feed gas stream containing methane, at least one C2 component, and at least one C3 component into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 component. The system comprises a feed stream heat exchanger configured to cool the feed gas stream to a temperature sufficient to condense the majority of the at least one C3 component in the feed gas stream to produce a cooled feed stream. A separator vessel is located downstream from the first heat exchanger and configured to separate the cooled feed stream into a separator gas stream and a separator liquid stream. A
fractionation column is located downstream from the separator vessel and configured to receive at least a portion of both the separator gas and liquid streams and produce a fractionation column bottoms product and a fractionation column overhead residue gas stream. A deethanizer tower is located downstream from the separator vessel and configured to receive at least a portion of the fractionation column bottoms product and to produce a deethanizer bottoms stream compris-ing a majority of the at least one C3 component and a deethanizer overhead gas stream.
In still another embodiment of the present invention, there is provided a system for separating a feed gas stream containing methane, at least one C2 component, and at least one
In yet another embodiment of the present invention, there is provided a system for separating a feed gas stream containing methane, at least one C2 component, and at least one C3 component into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 component. The system comprises a feed stream heat exchanger configured to cool the feed gas stream to a temperature sufficient to condense the majority of the at least one C3 component in the feed gas stream to produce a cooled feed stream. A separator vessel is located downstream from the first heat exchanger and configured to separate the cooled feed stream into a separator gas stream and a separator liquid stream. A
fractionation column is located downstream from the separator vessel and configured to receive at least a portion of both the separator gas and liquid streams and produce a fractionation column bottoms product and a fractionation column overhead residue gas stream. A deethanizer tower is located downstream from the separator vessel and configured to receive at least a portion of the fractionation column bottoms product and to produce a deethanizer bottoms stream compris-ing a majority of the at least one C3 component and a deethanizer overhead gas stream.
In still another embodiment of the present invention, there is provided a system for separating a feed gas stream containing methane, at least one C2 component, and at least one
-5-C3 component into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 component. The system comprises a feed stream heat exchanger configured to cool the feed gas stream to a temperature sufficient to condense the majority of the at least one C3 conwonent therein to produce a cooled feed stream. A fractionation column is located downstream from the feed stream heat exchanger and is configured to receive the cooled feed stream and produce a fractionation column bottoms product and a fractionation column overhead residue gas stream. The fractionation column includes a reboiler configured to vaporize at least a portion of the fractionation column liquid and reintroduce the vaporized fractionation column liquid back into the fractionation column. A deethanizer tower is located downstream from the fractionation column and configured to receive at least another portion of the fractionation column bottoms product and produce a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream. A deethanizer heat exchanger is provided and configured to receive and cool the deethanizer overhead gas stream. A deethanizer separation vessel is located downstream from the deethanizer heat exchanger and is configured to separate the cooled deethanizer overhead gas stream into a deethanizer liquid reflux stream and a deethanizer residue gas stream. Optionally, the system further includes a conduit configured to merge at least a portion of the deethanizer residue gas stream with at least a portion of the fractionation column overhead residue gas stream to form a combined residue gas stream. A
residue gas heat exchanger is provided and configured to condense at least a portion of the combined residue stream to form a residue gas reflux stream. Conduit is configured to deliver at least a portion of the residue gas reflux stream from the gas condensation unit to the fractionation column.
In even a further embodiment, there is provided a system for separating a feed gas stream containing methane, at least one C2 component, and at least one C3 component into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 component. The system comprises a feed stream heat exchanger configured to cool the feed gas stream to a temperature sufficient to condense the majority of the at least one C3 component in the feed gas stream to produce a cooled feed stream. A fractionation column is located downstream from the heat exchanger and is configured to receive the cooled feed stream and produce a
residue gas heat exchanger is provided and configured to condense at least a portion of the combined residue stream to form a residue gas reflux stream. Conduit is configured to deliver at least a portion of the residue gas reflux stream from the gas condensation unit to the fractionation column.
In even a further embodiment, there is provided a system for separating a feed gas stream containing methane, at least one C2 component, and at least one C3 component into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 component. The system comprises a feed stream heat exchanger configured to cool the feed gas stream to a temperature sufficient to condense the majority of the at least one C3 component in the feed gas stream to produce a cooled feed stream. A fractionation column is located downstream from the heat exchanger and is configured to receive the cooled feed stream and produce a
-6-fractionation column bottoms product and a fractionation column overhead residue gas stream. A deethanizer tower is located downstream from the fractionation column and configured to receive at least a portion of the fractionation column bottoms product and produce a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream. A deethanizer heat exchanger is provided and configured to receive and cool the deethanizer overhead gas stream. A
deethanizer separa-tion vessel is provided and configured to separate the cooled deethanizer overhead gas stream into a deethanizer liquid reflux stream and a deethanizer residue gas stream.
Conduit is provided and configured to deliver at least a portion of the deethanizer liquid reflux stream to the fractionation column. A residue gas heat exchanger is provided and configured to condense at least a portion of the fractionation column overhead residue gas stream. Conduit is provided and configured to deliver at least a portion of the condensed fractionation column overhead residue gas stream to the fractionation column.
BRIEF DESCRIPTION OF THE DRAWINGS
Figure 1 is a schematic diagram of a process according to one embodiment of the present invention; and Fig. 2 is a schematic diagram of a process according to another embodiment of the present invention.
DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT
Turning to Fig. 1, an embodiment of the present invention is shown that is particularly adapted for the recovery of C3 and heavier components from a hydrocarbon-containing gas stream, such as a natural gas or refinery gas stream. In particular embodiments, the inlet feed gas stream 10 comprises methane, at least one C2 component, at least one C3 component, and optionally heavier components. In still other embodiments, inlet feed gas stream 10 comprises methane as the predominant component, with C2, C3, and heavier components being present in lesser amounts. In refinery applications, the feed may also contain significant quantities of lighter components such as hydrogen. Particularly, in certain applications, the feed stream may comprise as much as 10%, or even as much as 50%, hydrogen.
deethanizer separa-tion vessel is provided and configured to separate the cooled deethanizer overhead gas stream into a deethanizer liquid reflux stream and a deethanizer residue gas stream.
Conduit is provided and configured to deliver at least a portion of the deethanizer liquid reflux stream to the fractionation column. A residue gas heat exchanger is provided and configured to condense at least a portion of the fractionation column overhead residue gas stream. Conduit is provided and configured to deliver at least a portion of the condensed fractionation column overhead residue gas stream to the fractionation column.
BRIEF DESCRIPTION OF THE DRAWINGS
Figure 1 is a schematic diagram of a process according to one embodiment of the present invention; and Fig. 2 is a schematic diagram of a process according to another embodiment of the present invention.
DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT
Turning to Fig. 1, an embodiment of the present invention is shown that is particularly adapted for the recovery of C3 and heavier components from a hydrocarbon-containing gas stream, such as a natural gas or refinery gas stream. In particular embodiments, the inlet feed gas stream 10 comprises methane, at least one C2 component, at least one C3 component, and optionally heavier components. In still other embodiments, inlet feed gas stream 10 comprises methane as the predominant component, with C2, C3, and heavier components being present in lesser amounts. In refinery applications, the feed may also contain significant quantities of lighter components such as hydrogen. Particularly, in certain applications, the feed stream may comprise as much as 10%, or even as much as 50%, hydrogen.
-7-The present invention exhibits the flexibility to accommodate a wide variety of feed pressures. In one embodiment, the feed stream 10 can be supplied at a pressure of at least 300 psi, or particularly, between about 350 psi to about 700 psi. Typically, feed stream 10 will be supplied at a temperature that is above the condensation point for the C3 components present therein; thercfore, feed stream will need to be cooled in order to condense these components. In this embodiment, feed gas stream 10 is passed through a heat exchanger 12 where it is cooled to a temperature sufficient to condense the majority of the at least one C3 component in the feed gas stream to produce a cooled gas feed stream. Note, the use of the word "gas" in the term "cooled gas feed stream" should not be taken as implying that the entirety of the stream is present in the gaseous state. Certain components, particularly the heavier components may be present as liquids. The cooling streams used in heat exchanger 12 are discussed in greater detail below. It will be understood that the heat exchange function shown schematically in heat exchanger 12 may be accomplished in a single or a plurality of heat exchange vessels.
The cooled inlet gas is passed via a line or conduit 14 to a separation vessel 16 where it is separated into a vapor stream 18 and a bottoms stream 20. Vapor stream 18 is directed toward an expander 22 to reduce the pressure of and further cool the stream.
The expanded vapor stream is passed via a line 24 to a fractionation column 26 containing one or more theoretical stages of mass transfer. In certain embodiments, the fractionation column 26 is a conventional distillation column containing a plurality of vertically spaced trays, one or more packed beds. or some combination of trays and packing.
The bottoms stream 20 recovered from separator vessel 16 contains primarily C3 and heavier components, although the bottoms stream 20 will also contain quantities of lighter materials. As explained further below, ultimately these lighter components will be separated from the C3 and heavier components in subsequent processing steps. In order to maximize the efficiency of those subsequent processing steps, the present embodiment seeks to control the levels of C2 and lighter components contained in the liquid, predominantly C3 stream that will be further processed. Thus, bottoms stream 20 is also passed to fractionation column 26.
Generally, bottoms stream 20 is introduced into fractionation column 26 below the introduc-tion point for the expanded vapor stream carried by line 24, although the arrangement of the introduction points for the various streams fed to fractionation column 26 can be varied as deemed appropriate. This step of introducing bottoms stream 20 into fractionation column
The cooled inlet gas is passed via a line or conduit 14 to a separation vessel 16 where it is separated into a vapor stream 18 and a bottoms stream 20. Vapor stream 18 is directed toward an expander 22 to reduce the pressure of and further cool the stream.
The expanded vapor stream is passed via a line 24 to a fractionation column 26 containing one or more theoretical stages of mass transfer. In certain embodiments, the fractionation column 26 is a conventional distillation column containing a plurality of vertically spaced trays, one or more packed beds. or some combination of trays and packing.
The bottoms stream 20 recovered from separator vessel 16 contains primarily C3 and heavier components, although the bottoms stream 20 will also contain quantities of lighter materials. As explained further below, ultimately these lighter components will be separated from the C3 and heavier components in subsequent processing steps. In order to maximize the efficiency of those subsequent processing steps, the present embodiment seeks to control the levels of C2 and lighter components contained in the liquid, predominantly C3 stream that will be further processed. Thus, bottoms stream 20 is also passed to fractionation column 26.
Generally, bottoms stream 20 is introduced into fractionation column 26 below the introduc-tion point for the expanded vapor stream carried by line 24, although the arrangement of the introduction points for the various streams fed to fractionation column 26 can be varied as deemed appropriate. This step of introducing bottoms stream 20 into fractionation column
8 26 provides an opportunity for the lighter materials co-absorbed in liquid bottoms stream 20 to be separated therefrom. Fractionation column 26 is equipped with an optional reboiler 28 to assist with separation of the C2 and lighter components from the bottoms of the fractiona-tion column. A portion of the fractionation column liquids taken from the bottom or near the bottom of column 26 are directed to reboiler 28 and at least partially vaporized and then reintroduced into the fractionation column 26. Accordingly, as the liquid stream exiting fractionation column 26 contains fewer C2 or lighter components, it has higher condensation temperature than the stream 20. This permits a propane refrigerant, or similar refrigerant, to be used to condense the overhead stream ti-om a deethanizer 36, which is discussed in greater detail below. Otherwise, if the bottoms product from fractionation column 26 contained a higher level of C2 or lighter components, a colder and therefore more expensive refrigeration system would need to be employed.
In fractionation column 26, a liquid bottoms stream comprising primarily Cl and heavier components plus some light components is recovered via a line 30 and a pump 32 and pumped via a line 34 to heat exchanger 12 where it is used to cool the inlet gas stream in line 10. The stream in line 34 is then passed to a deethanizer 36. In deethanizer 36 the stream from line 34 is separated by conventional distillation techniques as well known to the art for deethanizers into an overhead vapor stream 38 and a bottoms stream 40.
Deethanizer 36 also comprises a conventional reboiler 42. The stream recovered from deethanizer 36 through line 40 comprises primarily C3 and heavier components. An overhead stream is recovered from the deethanizer via line 38, which is rich in C2 and lighter components and is passed to a heat exchanger 44 where it is partially condensed and then through a line 46 to a separator 48.
From separator 48, a liquid stream is withdrawn via a line 50 and passed to a pump 52 from which a portion of the liquid stream is passed via a line 54 into an upper portion of deethanizer 36 as a reflux. The vapor stream recovered from separator 48 is passed via a line 56.
Deethanizer 36 is maintained at a higher pressure than fractionation column 26. The increased pressure for deethanizer 36 is supplied by pump 32 and maintained by a valve 57 disposed in line 56. In certain embodiments, the pressure in deethanizer 36 is at least 25 psi, or at least 100 psi, or at least 200 psi greater than the pressure in fractionation column 26.
A second portion of the liquid stream from separator 48 is passed via a line 58, through a heat exchanger 60, and into an upper portion of fractionation column 26, An
In fractionation column 26, a liquid bottoms stream comprising primarily Cl and heavier components plus some light components is recovered via a line 30 and a pump 32 and pumped via a line 34 to heat exchanger 12 where it is used to cool the inlet gas stream in line 10. The stream in line 34 is then passed to a deethanizer 36. In deethanizer 36 the stream from line 34 is separated by conventional distillation techniques as well known to the art for deethanizers into an overhead vapor stream 38 and a bottoms stream 40.
Deethanizer 36 also comprises a conventional reboiler 42. The stream recovered from deethanizer 36 through line 40 comprises primarily C3 and heavier components. An overhead stream is recovered from the deethanizer via line 38, which is rich in C2 and lighter components and is passed to a heat exchanger 44 where it is partially condensed and then through a line 46 to a separator 48.
From separator 48, a liquid stream is withdrawn via a line 50 and passed to a pump 52 from which a portion of the liquid stream is passed via a line 54 into an upper portion of deethanizer 36 as a reflux. The vapor stream recovered from separator 48 is passed via a line 56.
Deethanizer 36 is maintained at a higher pressure than fractionation column 26. The increased pressure for deethanizer 36 is supplied by pump 32 and maintained by a valve 57 disposed in line 56. In certain embodiments, the pressure in deethanizer 36 is at least 25 psi, or at least 100 psi, or at least 200 psi greater than the pressure in fractionation column 26.
A second portion of the liquid stream from separator 48 is passed via a line 58, through a heat exchanger 60, and into an upper portion of fractionation column 26, An
-9-overhead vapor stream recovered from the upper portion of fractionation column 26 is passed via a line 62, through heat exchanger 66 and then combined with the stream in line 56. It is noted that the stream carried by line 56 is flashed across valve 57. The combined stream contains a residue gas that comprises a major portion of the C., and lighter components from the inlet gas feed stream. This stream is passed via line 64 through heat exchanger 12 so as to provide cooling for feed stream 10. Alternatively, stream 56 and stream 62 can be passed separately through heat exchanger 12 such that stream 56, which contains a significant quantity of C7 components, would be available for internal use thus reducing the C2 content of the residue gas.
The cooling to heat exchanger 12 provided by the materials carried by lines 34 and 64 can be supplemented by a refrigerant, such as propane, supplied to heat exchanger 12 by line 76. Next, the residue gas carried by line 64 is passed through a compressor 66. The residue gas exits compressor 66 via line 68. Optionally, a portion of the residue gas carried by line 68 is passed via a line 70 to a heat exchanger 72 where it is cooled and condensed. In the embodiment illustrated, the chilled portion of residue gas exiting heat exchanger 72 is refluxed to the top of fractionation column 26. The other portion of residue gas from line 68 is withdrawn from the system via line 74. In those embodiments in which streams 56 and 62 are not combined and an additional reflux is desired for column 26, a portion of the contents of stream 62 are compressed, condensed and refluxed to the column.
In an illustrative embodiment of the process shown in Fig. 1, a dehydrated gas stream
The cooling to heat exchanger 12 provided by the materials carried by lines 34 and 64 can be supplemented by a refrigerant, such as propane, supplied to heat exchanger 12 by line 76. Next, the residue gas carried by line 64 is passed through a compressor 66. The residue gas exits compressor 66 via line 68. Optionally, a portion of the residue gas carried by line 68 is passed via a line 70 to a heat exchanger 72 where it is cooled and condensed. In the embodiment illustrated, the chilled portion of residue gas exiting heat exchanger 72 is refluxed to the top of fractionation column 26. The other portion of residue gas from line 68 is withdrawn from the system via line 74. In those embodiments in which streams 56 and 62 are not combined and an additional reflux is desired for column 26, a portion of the contents of stream 62 are compressed, condensed and refluxed to the column.
In an illustrative embodiment of the process shown in Fig. 1, a dehydrated gas stream
10 is charged to the process at 340 psia and 114F. The gas stream is cooled in heat exchanger 12 to a temperature of -66F and 330 psia and charged to separation vessel 16. In separation vessel 16, gaseous overhead stream 18 is produced and passed through expander 22 and is carried by line 24 at -99F and 150 psia to fractionation column 26.
The liquid stream recovered via line 20 at -1.5F and 145 psia and directed through pump 32 where its pressure is increased to 360 psia. The stream carried by line 34 is used to provide refrigera-tion to heat exchanger 12 and then directed to deethanizer 36 at a temperature of 74F and 355 psia.
In deethanizer 36, a bottoms liquid stream composed primarily of C3 and heavier components is recovered via a line 40 at a temperature of 173F at 350 psia.
The vapor stream recovered via line 56 is at a temperature of 24F at 335 psia. In the current simulation, the vapor stream recovered via line 56 was withdrawn from the system and used as fuel gas.
However, as illustrated in Fig. 1, this stream can be flashed across valve 57 and combined with the gas carried by line 62. A liquid reflux stream carried by line 58 is withdrawn from the deethanizer at a temperature of 24F and 335 psia. This stream is cooled, expanded, and refluxed to fractionation column 26 at -11rF and 145 psia.
The overhead vapor from fractionation column 26 carried by line 62 is at a tempera-ture of -117F and a pressure of 140 psia and is heat exchanged with the stream carried by line 58 and emerges from heat exchanger 60 at -99F and 135 psia and directed to heat exchanger 12 via line 64. This residue gas stream exits heat exchanger 12 at 95F and 125 psia and is directed toward compressor 66 (in this simulation a series of compressor stages with intercooling) where it is boosted to 1265 psia and its temperature raised to 115F. A portion of this compressed stream is withdrawn via line 70, cooled and condensed by heat exchanger 72 and refluxed to fractionation column 26 at a temperature of -112F and pressure of 1255 psia.
While specific temperatures have been referred to in connection with the embodiment illustrated in Fig. 1, it should be understood that a wide range of temperature and pressure variations are possible within the scope of the present invention. Such temperature and pressure variations are readily determined by those skilled in the art based upon the composi-tion of the specific feed streams, the desired recoveries and the like within the scope of the processes disclosed above.
Figure 2 illustrates another embodiment of a process in accordance with the present invention. Note, when applicable, the same reference numerals used in the description of Fig. 1 have been used to identify comparable lines or equipment. In the process of Fig. 2, the inlet gas stream is charged to the process via a line 10. The inlet feed gas is cooled in a heat exchanger 12 and thereafter passed via a line 14 to a heat exchanger 15 where it is further cooled to a selected temperature and passed via line 17 to a fractionation column 26 containing one or more theoretical stages of mass transfer. Fractionation column 26 is equipped with a reboiler 28 to assist with separation of the C2 and lighter components from the bottoms of the fractionation column. A portion of the tower liquid from fractionation column 26 is directed to reboiler 28 and at least partially vaporized and then reintroduced into the bottom of fractionation column 26.
In fractionation column 26, a liquid bottoms product comprising primarily C3 and heavier components plus some light components is recovered via a line 30 and a pump 32 and
The liquid stream recovered via line 20 at -1.5F and 145 psia and directed through pump 32 where its pressure is increased to 360 psia. The stream carried by line 34 is used to provide refrigera-tion to heat exchanger 12 and then directed to deethanizer 36 at a temperature of 74F and 355 psia.
In deethanizer 36, a bottoms liquid stream composed primarily of C3 and heavier components is recovered via a line 40 at a temperature of 173F at 350 psia.
The vapor stream recovered via line 56 is at a temperature of 24F at 335 psia. In the current simulation, the vapor stream recovered via line 56 was withdrawn from the system and used as fuel gas.
However, as illustrated in Fig. 1, this stream can be flashed across valve 57 and combined with the gas carried by line 62. A liquid reflux stream carried by line 58 is withdrawn from the deethanizer at a temperature of 24F and 335 psia. This stream is cooled, expanded, and refluxed to fractionation column 26 at -11rF and 145 psia.
The overhead vapor from fractionation column 26 carried by line 62 is at a tempera-ture of -117F and a pressure of 140 psia and is heat exchanged with the stream carried by line 58 and emerges from heat exchanger 60 at -99F and 135 psia and directed to heat exchanger 12 via line 64. This residue gas stream exits heat exchanger 12 at 95F and 125 psia and is directed toward compressor 66 (in this simulation a series of compressor stages with intercooling) where it is boosted to 1265 psia and its temperature raised to 115F. A portion of this compressed stream is withdrawn via line 70, cooled and condensed by heat exchanger 72 and refluxed to fractionation column 26 at a temperature of -112F and pressure of 1255 psia.
While specific temperatures have been referred to in connection with the embodiment illustrated in Fig. 1, it should be understood that a wide range of temperature and pressure variations are possible within the scope of the present invention. Such temperature and pressure variations are readily determined by those skilled in the art based upon the composi-tion of the specific feed streams, the desired recoveries and the like within the scope of the processes disclosed above.
Figure 2 illustrates another embodiment of a process in accordance with the present invention. Note, when applicable, the same reference numerals used in the description of Fig. 1 have been used to identify comparable lines or equipment. In the process of Fig. 2, the inlet gas stream is charged to the process via a line 10. The inlet feed gas is cooled in a heat exchanger 12 and thereafter passed via a line 14 to a heat exchanger 15 where it is further cooled to a selected temperature and passed via line 17 to a fractionation column 26 containing one or more theoretical stages of mass transfer. Fractionation column 26 is equipped with a reboiler 28 to assist with separation of the C2 and lighter components from the bottoms of the fractionation column. A portion of the tower liquid from fractionation column 26 is directed to reboiler 28 and at least partially vaporized and then reintroduced into the bottom of fractionation column 26.
In fractionation column 26, a liquid bottoms product comprising primarily C3 and heavier components plus some light components is recovered via a line 30 and a pump 32 and
-11-pumped via a line 34 to heat exchanger 12 where it is used to cool the inlet gas stream in line 10. The stream in line 34 is then passed via to a deethanizer 36. In deethanizer 32 the stream from line 34 is separated by conventional distillation techniques into an overhead vapor stream 38 and a bottoms stream 40. A conventional reboiler 42 is shown for with-drawing a portion of the deethanizer tower liquid, at least partially vaporizing the withdrawn portion, and returning the at least partially vaporized stream back to deethanizer 36. The stream recovered from deethanizer 36 through line 40 comprises primarily C3 and heavier components. An overhead stream is recovered from the deethanizer via line 38, which is rich in C2 and lighter components and is passed to a heat exchanger 44 where it is at least partially condensed and then through a line 46 to a separator 48. From separator 48, a liquid stream is withdrawn via a line 50 and passed to a pump 52 from which a portion of the liquid stream is passed via a line 54 into an upper portion of deethanizer 36 as a reflux. The vapor stream recovered from separator 48 is passed via a line 56 and through an expansion valve 57.
The vapor stream is then combined with the residue gas from line 62 and directed toward a compressor 66 via line 64.
A second portion of the liquid stream from separator 48 is passed via a line 58 and a heat exchanger 60 into an upper portion of fractionation column 26. An overhead vapor stream recovered from the upper portion of fractionation column 26 is passed via a line 62 through heat exchanger 60 to combination with the stream in line 26. The combined stream carried by line 64 contains a major portion of the C2 and lighter components from the inlet gas feed stream. As noted above, the stream in line 64 is compressed by compressor 66 arid passed into line 68. A portion of the compressed residue gas carried by line 68 is passed via a line 70 to a heat exchanger 72 where it is cooled and condensed. In the embodiment illustrated, the condensed portion of residue gas exiting heat exchanger 72 is refluxed to the top of fractionation column 26. The other portion of residue gas from line 68 is withdrawn from the system via line 74.
It is noted that, as discussed above with respect to Fig. 1, in certain embodiments, streams 56 and 62 may be kept separate. When an additional reflux is desired for column 26, a slip stream of the material carried by line 62 can be compressed, condensed, and refluxed to the column. It is also noted that for any embodiment discussed above, it is within the scope of the present invention for the residue gas reflux carried by line 70 to be used without equipping fractionation column 26 with a reboiler 28.
The vapor stream is then combined with the residue gas from line 62 and directed toward a compressor 66 via line 64.
A second portion of the liquid stream from separator 48 is passed via a line 58 and a heat exchanger 60 into an upper portion of fractionation column 26. An overhead vapor stream recovered from the upper portion of fractionation column 26 is passed via a line 62 through heat exchanger 60 to combination with the stream in line 26. The combined stream carried by line 64 contains a major portion of the C2 and lighter components from the inlet gas feed stream. As noted above, the stream in line 64 is compressed by compressor 66 arid passed into line 68. A portion of the compressed residue gas carried by line 68 is passed via a line 70 to a heat exchanger 72 where it is cooled and condensed. In the embodiment illustrated, the condensed portion of residue gas exiting heat exchanger 72 is refluxed to the top of fractionation column 26. The other portion of residue gas from line 68 is withdrawn from the system via line 74.
It is noted that, as discussed above with respect to Fig. 1, in certain embodiments, streams 56 and 62 may be kept separate. When an additional reflux is desired for column 26, a slip stream of the material carried by line 62 can be compressed, condensed, and refluxed to the column. It is also noted that for any embodiment discussed above, it is within the scope of the present invention for the residue gas reflux carried by line 70 to be used without equipping fractionation column 26 with a reboiler 28.
-12-While the present invention has been described by reference to certain of its preferred embodiments, it is respectfully pointed out that the embodiments described are illustrative rather than limiting in nature and that many variations and modifications are possible within the scope of the present invention.
Claims (21)
1. A process for separating a feed gas stream containing methane, at least one C2 component, and at least one C3 component into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 component, the process comprising:
a) cooling the feed gas stream to a temperature sufficient to condense the majori-ty of the at least one C3 component in the feed gas stream to produce a cooled feed stream;
b) introducing the cooled feed stream into a separator vessel to separate the cooled feed stream into a separator gas stream and a separator liquid stream;
c) introducing at least a portion of both of the separator gas and liquid streams from the separator vessel into a fractionation column to produce a fractiona-tion column bottoms product and a fractionation column overhead residue gas stream;
d) introducing the fractionation column bottoms product into a deethanizer tower and producing a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream;
e) cooling and at least partially condensing the deethanizer overhead gas stream thereby producing a deethanizer liquid reflux stream and a deethanizer residue gas stream; and f) introducing at least a portion of the deethanizer liquid reflux stream into the fractionation column.
a) cooling the feed gas stream to a temperature sufficient to condense the majori-ty of the at least one C3 component in the feed gas stream to produce a cooled feed stream;
b) introducing the cooled feed stream into a separator vessel to separate the cooled feed stream into a separator gas stream and a separator liquid stream;
c) introducing at least a portion of both of the separator gas and liquid streams from the separator vessel into a fractionation column to produce a fractiona-tion column bottoms product and a fractionation column overhead residue gas stream;
d) introducing the fractionation column bottoms product into a deethanizer tower and producing a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream;
e) cooling and at least partially condensing the deethanizer overhead gas stream thereby producing a deethanizer liquid reflux stream and a deethanizer residue gas stream; and f) introducing at least a portion of the deethanizer liquid reflux stream into the fractionation column.
2. The process according to claim 1, wherein the fractionation column further includes a reboiler operable to vaporize at least a portion of a fractionation column liquid, the vaporized fractionation column liquid being reintroduced into the fractionation column.
3. The process according to claim I, further comprising:
g) combining the fractionation column overhead residue gas stream with at least a portion of the deethanizer residue gas stream to form a combined residue gas stream;
h) compressing and cooling at least a portion of the combined residue gas stream to produce a residue gas reflux stream; and i) introducing the residue gas reflux stream into the fractionation column.
g) combining the fractionation column overhead residue gas stream with at least a portion of the deethanizer residue gas stream to form a combined residue gas stream;
h) compressing and cooling at least a portion of the combined residue gas stream to produce a residue gas reflux stream; and i) introducing the residue gas reflux stream into the fractionation column.
4. The process according to claim 1, wherein the process further comprises:
g) compressing and cooling at least a portion of the fractionation column over-head residue gas stream to produce a residue gas reflux stream; and h) introducing the residue gas reflux stream into the fractionation column.
g) compressing and cooling at least a portion of the fractionation column over-head residue gas stream to produce a residue gas reflux stream; and h) introducing the residue gas reflux stream into the fractionation column.
5. A process for separating a feed gas stream containing methane, at least one C2 component, and at least one C3 component into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 component, the process comprising:
a) cooling the feed gas stream to a temperature sufficient to condense the majori-ty of the at least one C3 component in the feed gas stream to produce a cooled feed stream;
b) passing the cooled feed stream to a fractionation column to produce a liquid fractionation column bottoms product and a fractionation column overhead residue gas stream, the fractionation column including a reboiler operable to vaporize at least a portion of a fractionation column liquid, the vaporized frac-tionation column liquid being reintroduced into the fractionation column;
c) introducing the fractionation column bottoms product into a deethanizer tower and producing a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream;
d) cooling and at least partially condensing the deethanizer overhead gas stream thereby producing a deethanizer liquid reflux stream and a deethanizer residue gas stream; and e) introducing at least a portion of the deethanizer liquid reflux stream into the fractionation column.
a) cooling the feed gas stream to a temperature sufficient to condense the majori-ty of the at least one C3 component in the feed gas stream to produce a cooled feed stream;
b) passing the cooled feed stream to a fractionation column to produce a liquid fractionation column bottoms product and a fractionation column overhead residue gas stream, the fractionation column including a reboiler operable to vaporize at least a portion of a fractionation column liquid, the vaporized frac-tionation column liquid being reintroduced into the fractionation column;
c) introducing the fractionation column bottoms product into a deethanizer tower and producing a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream;
d) cooling and at least partially condensing the deethanizer overhead gas stream thereby producing a deethanizer liquid reflux stream and a deethanizer residue gas stream; and e) introducing at least a portion of the deethanizer liquid reflux stream into the fractionation column.
6. The process according to claim 5, wherein the process further comprises:
0 compressing and cooling at least a portion of the fractionation column over-head residue gas stream to produce a residue gas reflux stream; and g) introducing the residue gas reflux stream into the fractionation column.
0 compressing and cooling at least a portion of the fractionation column over-head residue gas stream to produce a residue gas reflux stream; and g) introducing the residue gas reflux stream into the fractionation column.
7. The process according to claim 6, wherein prior to step (b) introducing the cooled feed stream into a separator vessel to separate the cooled feed stream into a separator gas stream and a separator liquid stream.
8. The process according to claim 6, wherein the process further comprises, prior to step (0, combining at least a portion of the deethanizer residue gas stream with the at least a portion of the fractionation column overhead gas residue stream.
9. The process according to claim 8, wherein prior to step (b) introducing the cooled feed stream into a separator vessel to separate the cooled feed stream into a separator gas stream and a separator liquid stream.
1 0. A process for separating a feed gas stream containing methane, at least one C2 component, and at least one C3 component into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 component, the process comprising:
a) cooling the feed gas stream to a temperature sufficient to condense the majori-ty of the at least one C3 component in the feed gas stream to produce a cooled feed stream;
b) passing the cooled feed stream to a fractionation column to produce a liquid fractionation column bottoms product and a fractionation column overhead residue gas stream, c) introducing the fractionation column bottoms product into a deethanizer tower and producing a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream;
d) cooling and at least partially condensing the deethanizer overhead gas stream thereby producing a deethanizer liquid reflux stream and a deethanizer residue gas stream;
e) introducing at least a portion of the deethanizer liquid reflux stream into the fractionation column;
compressing and cooling at least a portion of the fractionation column over-head residue gas stream to produce a residue gas reflux stream; and introducing the residue gas reflux stream into the fractionation column.
a) cooling the feed gas stream to a temperature sufficient to condense the majori-ty of the at least one C3 component in the feed gas stream to produce a cooled feed stream;
b) passing the cooled feed stream to a fractionation column to produce a liquid fractionation column bottoms product and a fractionation column overhead residue gas stream, c) introducing the fractionation column bottoms product into a deethanizer tower and producing a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream;
d) cooling and at least partially condensing the deethanizer overhead gas stream thereby producing a deethanizer liquid reflux stream and a deethanizer residue gas stream;
e) introducing at least a portion of the deethanizer liquid reflux stream into the fractionation column;
compressing and cooling at least a portion of the fractionation column over-head residue gas stream to produce a residue gas reflux stream; and introducing the residue gas reflux stream into the fractionation column.
11. The process according to claim 10, wherein prior to step (f), at least a portion of the deethanizer overhead gas stream is combined with the fractionation column overhead residue gas stream.
12. A system for separating a feed gas stream containing methane, at least one C2 component, and at least one C3 component into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 component, the system comprising:
a) a feed stream heat exchanger configured to cool the feed gas stream to a tem-perature sufficient to condense the majority of the at least one C3 component in the feed gas stream to produce a cooled feed stream;
b) a separator vessel located downstream from the first heat exchanger and con-figured to separate the cooled feed stream into a separator gas stream and a separator liquid stream;
c) a fractionation column located downstream from the separator vessel and con-figured to receive at least a portion of both the separator gas and liquid streams and produce a fractionation column bottoms product and a fractionation col-umn overhead residue gas stream;
d) a deethanizer tower located downstream from the separator vessel and config-ured to receive at least a portion of the fractionation column bottoms product and produce a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream;
e) a deethanizer heat exchanger configured to receive and cool the deethanizer overhead gas stream; and a deethanizer separation vessel configured to separate the cooled deethanizer overhead gas stream into a deethanizer liquid reflux stream and a deethanizer residue gas stream.
a) a feed stream heat exchanger configured to cool the feed gas stream to a tem-perature sufficient to condense the majority of the at least one C3 component in the feed gas stream to produce a cooled feed stream;
b) a separator vessel located downstream from the first heat exchanger and con-figured to separate the cooled feed stream into a separator gas stream and a separator liquid stream;
c) a fractionation column located downstream from the separator vessel and con-figured to receive at least a portion of both the separator gas and liquid streams and produce a fractionation column bottoms product and a fractionation col-umn overhead residue gas stream;
d) a deethanizer tower located downstream from the separator vessel and config-ured to receive at least a portion of the fractionation column bottoms product and produce a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream;
e) a deethanizer heat exchanger configured to receive and cool the deethanizer overhead gas stream; and a deethanizer separation vessel configured to separate the cooled deethanizer overhead gas stream into a deethanizer liquid reflux stream and a deethanizer residue gas stream.
13. The system according to claim 12, wherein the fractionation column further includes a reboiler configured to vaporize at least a portion of a fractionation column liquid and reintroduce the vaporized fractionation column liquid back into the fractionation column.
14. The system according to claim 12, further comprising:
conduit configured to merge at least a portion of the deethanizer residue gas stream with at least a portion of the fractionation column overhead residue gas stream to form a combined residue gas stream;
h) a residue gas heat exchanger configured to receive at least a portion of the combined residue gas stream and to produce a residue gas reflux stream; and i) conduit configured to deliver at least a portion of the residue gas reflux stream from the residue gas heat exchanger to the fractionation column.
conduit configured to merge at least a portion of the deethanizer residue gas stream with at least a portion of the fractionation column overhead residue gas stream to form a combined residue gas stream;
h) a residue gas heat exchanger configured to receive at least a portion of the combined residue gas stream and to produce a residue gas reflux stream; and i) conduit configured to deliver at least a portion of the residue gas reflux stream from the residue gas heat exchanger to the fractionation column.
15. The system according to claim 12, further comprising:
a compressor located upstream from the residue gas heat exchanger and con-figured to compress the combined residue gas stream.
a compressor located upstream from the residue gas heat exchanger and con-figured to compress the combined residue gas stream.
16. A system for separating a feed gas stream containing methane, at least one C2 component, and at least one C3 component into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 component, the system comprising:
a) a feed stream heat exchanger configured to cool the feed gas stream to a tem-perature sufficient to condense the majority of the at least one C3 component in the feed gas stream to produce a cooled feed stream;
b) a fractionation column configured to receive the cooled feed stream and pro-duce a fractionation column bottoms product and a fractionation column overhead residue gas stream, the fractionation column including a reboiler configured to vaporize at least a portion of a fractionation column liquid and reintroduce the vaporized fractionation column liquid back into the fractiona-tion column;
c) a deethanizer tower located downstream from the fractionation column and configured to receive at least another portion of the fractionation column bot-toms product and produce a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream;
d) a deethanizer heat exchanger configured to receive and cool the deethanizer overhead gas stream; and e) a deethanizer separation vessel configured to separate the cooled deethanizer overhead gas stream into a deethanizer liquid reflux stream and a deethanizer residue gas stream.
a) a feed stream heat exchanger configured to cool the feed gas stream to a tem-perature sufficient to condense the majority of the at least one C3 component in the feed gas stream to produce a cooled feed stream;
b) a fractionation column configured to receive the cooled feed stream and pro-duce a fractionation column bottoms product and a fractionation column overhead residue gas stream, the fractionation column including a reboiler configured to vaporize at least a portion of a fractionation column liquid and reintroduce the vaporized fractionation column liquid back into the fractiona-tion column;
c) a deethanizer tower located downstream from the fractionation column and configured to receive at least another portion of the fractionation column bot-toms product and produce a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream;
d) a deethanizer heat exchanger configured to receive and cool the deethanizer overhead gas stream; and e) a deethanizer separation vessel configured to separate the cooled deethanizer overhead gas stream into a deethanizer liquid reflux stream and a deethanizer residue gas stream.
17. The system according to claim 16, the system further comprising:
a residue gas heat exchanger configured to condense at least a portion of the fractionation column overhead residue gas stream to form a residue gas reflux stream; and conduit configured to deliver at least a portion of the residue gas reflux stream from the residue gas heat exchanger to the fractionation column.
a residue gas heat exchanger configured to condense at least a portion of the fractionation column overhead residue gas stream to form a residue gas reflux stream; and conduit configured to deliver at least a portion of the residue gas reflux stream from the residue gas heat exchanger to the fractionation column.
18. The system according to claim 16, further comprising:
0 a compressor located upstream from the residue gas heat exchanger and con-figured to compress the fractionation column overhead residue gas stream.
0 a compressor located upstream from the residue gas heat exchanger and con-figured to compress the fractionation column overhead residue gas stream.
19. The system according to claim 16, further comprising:
conduit configured to merge at least a portion of the deethanizer residue gas stream with at least the fractionation column overhead residue gas stream to form a combined residue gas stream.
conduit configured to merge at least a portion of the deethanizer residue gas stream with at least the fractionation column overhead residue gas stream to form a combined residue gas stream.
20. A system for separating a feed gas stream containing methane, at least one C2 component, and at least one C3 component into a volatile gas stream containing a major portion of the methane and at least one C2 component and a less volatile stream containing a major portion of the at least one C3 component, the system comprising:
a) a feed stream heat exchanger configured to cool the feed gas stream to a tem-perature sufficient to condense the majority of the at least one C3 component in the feed gas stream to produce a cooled feed stream;
b) a fractionation column configured to receive the cooled feed stream and pro-duce a fractionation column bottoms product and a fractionation column overhead residue gas stream;
c) a deethanizer tower located downstream from the fractionation column and configured to receive at least a portion of the fractionation column bottoms product and produce a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream;
d) a deethanizer heat exchanger configured to receive and cool the deethanizer overhead gas stream;
e) a deethanizer separation vessel configured to separate the cooled deethanizer overhead gas stream into a deethanizer liquid reflux stream and a deethanizer residue gas stream;
conduit configured to deliver at least a portion of the deethanizer liquid reflux stream to the fractionation column;
a residue gas heat exchanger configured to condense at least a portion of the fractionation column overhead residue gas stream; and h) conduit configured to deliver at least a portion of the condensed fractionation column overhead residue gas stream to the fractionation column.
a) a feed stream heat exchanger configured to cool the feed gas stream to a tem-perature sufficient to condense the majority of the at least one C3 component in the feed gas stream to produce a cooled feed stream;
b) a fractionation column configured to receive the cooled feed stream and pro-duce a fractionation column bottoms product and a fractionation column overhead residue gas stream;
c) a deethanizer tower located downstream from the fractionation column and configured to receive at least a portion of the fractionation column bottoms product and produce a deethanizer bottoms stream comprising a majority of the at least one C3 component and a deethanizer overhead gas stream;
d) a deethanizer heat exchanger configured to receive and cool the deethanizer overhead gas stream;
e) a deethanizer separation vessel configured to separate the cooled deethanizer overhead gas stream into a deethanizer liquid reflux stream and a deethanizer residue gas stream;
conduit configured to deliver at least a portion of the deethanizer liquid reflux stream to the fractionation column;
a residue gas heat exchanger configured to condense at least a portion of the fractionation column overhead residue gas stream; and h) conduit configured to deliver at least a portion of the condensed fractionation column overhead residue gas stream to the fractionation column.
21. The system according to claim 20, further comprising:
i) conduit configured to merge at least a portion of the deethanizer residue gas stream with at least the fractionation column overhead residue gas stream to form a combined residue gas stream.
i) conduit configured to merge at least a portion of the deethanizer residue gas stream with at least the fractionation column overhead residue gas stream to form a combined residue gas stream.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US36075310P | 2010-07-01 | 2010-07-01 | |
| US61/360,753 | 2010-07-01 | ||
| PCT/US2011/042654 WO2012003358A2 (en) | 2010-07-01 | 2011-06-30 | Methods and systems for recovering liquified petroleum gas from natural gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2805272A1 CA2805272A1 (en) | 2012-01-05 |
| CA2805272C true CA2805272C (en) | 2015-08-11 |
Family
ID=45398673
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2805272A Active CA2805272C (en) | 2010-07-01 | 2011-06-30 | Methods and systems for recovering liquified petroleum gas from natural gas |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US20120000245A1 (en) |
| AU (1) | AU2011272754B2 (en) |
| CA (1) | CA2805272C (en) |
| MY (1) | MY172490A (en) |
| WO (1) | WO2012003358A2 (en) |
Families Citing this family (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9243842B2 (en) | 2008-02-15 | 2016-01-26 | Black & Veatch Corporation | Combined synthesis gas separation and LNG production method and system |
| US10113127B2 (en) | 2010-04-16 | 2018-10-30 | Black & Veatch Holding Company | Process for separating nitrogen from a natural gas stream with nitrogen stripping in the production of liquefied natural gas |
| WO2012075266A2 (en) | 2010-12-01 | 2012-06-07 | Black & Veatch Corporation | Ngl recovery from natural gas using a mixed refrigerant |
| US10451344B2 (en) | 2010-12-23 | 2019-10-22 | Fluor Technologies Corporation | Ethane recovery and ethane rejection methods and configurations |
| FR2970258B1 (en) * | 2011-01-06 | 2014-02-07 | Technip France | PROCESS FOR PRODUCING C3 + HYDROCARBON RICH CUT AND METHANE ETHANE RICH CURRENT FROM HYDROCARBON RICH POWER CURRENT AND ASSOCIATED PLANT. |
| US10852060B2 (en) | 2011-04-08 | 2020-12-01 | Pilot Energy Solutions, Llc | Single-unit gas separation process having expanded, post-separation vent stream |
| US10139157B2 (en) | 2012-02-22 | 2018-11-27 | Black & Veatch Holding Company | NGL recovery from natural gas using a mixed refrigerant |
| US20140075987A1 (en) * | 2012-09-20 | 2014-03-20 | Fluor Technologies Corporation | Configurations and methods for ngl recovery for high nitrogen content feed gases |
| US10563913B2 (en) | 2013-11-15 | 2020-02-18 | Black & Veatch Holding Company | Systems and methods for hydrocarbon refrigeration with a mixed refrigerant cycle |
| GB201403560D0 (en) * | 2014-02-28 | 2014-04-16 | Eltek As | Inverter system |
| US9574822B2 (en) | 2014-03-17 | 2017-02-21 | Black & Veatch Corporation | Liquefied natural gas facility employing an optimized mixed refrigerant system |
| KR101550046B1 (en) * | 2014-04-09 | 2015-09-04 | 동아대학교 산학협력단 | Floating Liquefied Natural Gas Fractional Distillation Process Using Diabatic Divided Wall Column |
| WO2017075310A1 (en) * | 2015-10-29 | 2017-05-04 | Black & Veatch Holding Company | Enhanced low temperature separation process |
| US10006701B2 (en) | 2016-01-05 | 2018-06-26 | Fluor Technologies Corporation | Ethane recovery or ethane rejection operation |
| US10330382B2 (en) | 2016-05-18 | 2019-06-25 | Fluor Technologies Corporation | Systems and methods for LNG production with propane and ethane recovery |
| US10533794B2 (en) * | 2016-08-26 | 2020-01-14 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
| US10551118B2 (en) * | 2016-08-26 | 2020-02-04 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
| US10551119B2 (en) | 2016-08-26 | 2020-02-04 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
| BR112019003090A2 (en) | 2016-09-09 | 2019-05-21 | Fluor Technologies Corporation | methods and configuration for refurbishing ngl plant for high ethane recovery |
| CA3077409A1 (en) | 2017-10-20 | 2019-04-25 | Fluor Technologies Corporation | Phase implementation of natural gas liquid recovery plants |
| JP7051372B2 (en) * | 2017-11-01 | 2022-04-11 | 東洋エンジニアリング株式会社 | Hydrocarbon separation method and equipment |
| JP7043126B6 (en) * | 2017-11-06 | 2022-04-18 | 東洋エンジニアリング株式会社 | A device for separating and recovering multiple types of hydrocarbons from LNG |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2578637B1 (en) * | 1985-03-05 | 1987-06-26 | Technip Cie | PROCESS FOR FRACTIONATION OF GASEOUS LOADS AND INSTALLATION FOR CARRYING OUT THIS PROCESS |
| US4687499A (en) * | 1986-04-01 | 1987-08-18 | Mcdermott International Inc. | Process for separating hydrocarbon gas constituents |
| US5799507A (en) * | 1996-10-25 | 1998-09-01 | Elcor Corporation | Hydrocarbon gas processing |
| US6116050A (en) * | 1998-12-04 | 2000-09-12 | Ipsi Llc | Propane recovery methods |
| US6401486B1 (en) * | 2000-05-18 | 2002-06-11 | Rong-Jwyn Lee | Enhanced NGL recovery utilizing refrigeration and reflux from LNG plants |
| US6405561B1 (en) * | 2001-05-15 | 2002-06-18 | Black & Veatch Pritchard, Inc. | Gas separation process |
| US6516631B1 (en) * | 2001-08-10 | 2003-02-11 | Mark A. Trebble | Hydrocarbon gas processing |
| US6823692B1 (en) * | 2002-02-11 | 2004-11-30 | Abb Lummus Global Inc. | Carbon dioxide reduction scheme for NGL processes |
| US6662589B1 (en) * | 2003-04-16 | 2003-12-16 | Air Products And Chemicals, Inc. | Integrated high pressure NGL recovery in the production of liquefied natural gas |
| CA2543195C (en) * | 2003-10-30 | 2009-02-10 | Fluor Technologies Corporation | Flexible ngl process and methods |
| US7159417B2 (en) * | 2004-03-18 | 2007-01-09 | Abb Lummus Global, Inc. | Hydrocarbon recovery process utilizing enhanced reflux streams |
| US9869510B2 (en) * | 2007-05-17 | 2018-01-16 | Ortloff Engineers, Ltd. | Liquefied natural gas processing |
-
2011
- 2011-06-30 AU AU2011272754A patent/AU2011272754B2/en not_active Ceased
- 2011-06-30 MY MYPI2012005673A patent/MY172490A/en unknown
- 2011-06-30 WO PCT/US2011/042654 patent/WO2012003358A2/en active Application Filing
- 2011-06-30 US US13/174,002 patent/US20120000245A1/en not_active Abandoned
- 2011-06-30 CA CA2805272A patent/CA2805272C/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| US20120000245A1 (en) | 2012-01-05 |
| WO2012003358A2 (en) | 2012-01-05 |
| AU2011272754A1 (en) | 2013-01-17 |
| CA2805272A1 (en) | 2012-01-05 |
| AU2011272754B2 (en) | 2016-02-11 |
| WO2012003358A3 (en) | 2012-04-12 |
| MY172490A (en) | 2019-11-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA2805272C (en) | Methods and systems for recovering liquified petroleum gas from natural gas | |
| US10113127B2 (en) | Process for separating nitrogen from a natural gas stream with nitrogen stripping in the production of liquefied natural gas | |
| JP5997798B2 (en) | Nitrogen removal by isobaric open frozen natural gas liquid recovery | |
| EP1735257B1 (en) | Hydrocarbon gas processing for rich gas streams | |
| US6516631B1 (en) | Hydrocarbon gas processing | |
| CA2440142C (en) | Cryogenic process utilizing high pressure absorber column | |
| US5275005A (en) | Gas processing | |
| AU755559B2 (en) | A process for separating a multi-component pressurized feed stream using distillation | |
| CA2572430C (en) | Configurations and methods for gas condensate separation from high-pressure hydrocarbon mixtures | |
| US6405561B1 (en) | Gas separation process | |
| US20060218968A1 (en) | High propane recovery process and configurations | |
| WO2000023756A1 (en) | Volatile component removal process from natural gas | |
| AU2002338248A1 (en) | Cryogenic process utilizing high pressure absorber column | |
| NO313159B1 (en) | Process for separating out hydrocarbon gas components as well as plants for carrying out the same | |
| NO158478B (en) | PROCEDURE FOR SEPARATING NITROGEN FROM NATURAL GAS. | |
| KR20110010776A (en) | Iso-pressure open refrigeration ngl recovery | |
| WO2013055305A1 (en) | Process for separating nitrogen from a natural gas stream with nitrogen stripping in the production of liquefied natural gas | |
| US9487458B2 (en) | Configurations and methods for nitrogen rejection, LNG and NGL production from high nitrogen feed gases | |
| EP3052586B1 (en) | Split feed addition to iso-pressure open refrigeration lpg recovery | |
| AU2013204093B2 (en) | Iso-pressure open refrigeration NGL recovery | |
| AU2004210442B2 (en) | Removing natural gas liquids from a gaseous natural gas stream | |
| WO2017040161A1 (en) | Processes for stabilizing a liquid hydrocarbon stream |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request |
Effective date: 20130415 |