US20070227186A1 - Systems and methods for low-temperature gas separation - Google Patents

Systems and methods for low-temperature gas separation Download PDF

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Publication number
US20070227186A1
US20070227186A1 US11/233,378 US23337805A US2007227186A1 US 20070227186 A1 US20070227186 A1 US 20070227186A1 US 23337805 A US23337805 A US 23337805A US 2007227186 A1 US2007227186 A1 US 2007227186A1
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gas
flow
vapor stream
stream
liquid
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Vadim Alferov
Lev Bagirov
Vladimir Feygin
Salavat Imaev
Leonard Dmitriev
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3S GAS TECHNOLOGIES Ltd
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Individual
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Assigned to TRANSLANG TECHNOLOGIES LTD. reassignment TRANSLANG TECHNOLOGIES LTD. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: ALFEROV, VADIM IVANOVICH, BAGIROV, LEV ARKAD'EVICH, DMITRIEV, LEONARD MAKAROVICH, FEYGIN, VLADIMIR ISAAKOVICH, IMAEV, SALAVAT ZAINETDINOVICH
Publication of US20070227186A1 publication Critical patent/US20070227186A1/en
Assigned to 3S GAS TECHNOLOGIES LTD. reassignment 3S GAS TECHNOLOGIES LTD. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: TRANSLANG TECHNOLOGIES LTD.
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0033—Other features
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0033—Other features
    • B01D5/0045—Vacuum condensation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G7/00—Distillation of hydrocarbon oils
    • 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
    • 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
    • F25J3/0238—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 2 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
    • F25J2200/02—Processes or apparatus using separation by rectification in a single 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
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • 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
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/10—Processes or apparatus using other separation and/or other processing means using combined expansion and separation, e.g. in a vortex tube, "Ranque tube" or a "cyclonic fluid separator", i.e. combination of an isentropic nozzle and a cyclonic separator; Centrifugal separation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/04—Mixing or blending of fluids with 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/60—Expansion by ejector or injector, e.g. "Gasstrahlpumpe", "venturi mixing", "jet pumps"
    • 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
    • F25J2270/02—Internal 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
    • F25J2270/04—Internal refrigeration with work-producing gas expansion 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
    • F25J2270/88—Quasi-closed internal refrigeration or heat pump cycle, if not otherwise provided
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration

Definitions

  • the invention relates to gas separation techniques, and in particular to systems and methods for low-temperature gas separation.
  • the method of U.S. Pat. No. 6,182,468B1 consists of cooling of a mixture, expansion of the mixture without doing mechanical work, partial condensation of the mixture during its expansion, separation of the mixture or its part in the rectifying tower to obtain the products in liquid and gas phase.
  • cooling of the mixture is performed using recuperative heat exchangers and a chiller, while expansion of the mixture is achieved by means of mixture throttling in the Joule-Thomson valve.
  • Patent RU2047061C1 includes cooling of a mixture and its separation into vapor and liquid phases, expansion of one part of the vapor phase without doing mechanical work and that of the other part by doing mechanical work, separation of the expanded mixture in the rectifying tower to obtain gas and liquid products.
  • a method of low-temperature gas mixture separation suitable for separating components of a hydrocarbon gas mixture, including: cooling a gas mixture; condensing a gas mixture to produce a liquid stream and a gas/vapor; rectifying at least a portion of the liquid stream thereby producing respective gas-phase products; transferring heat energy to or from at least one of the liquid stream, the gas/vapor stream and gas-phase products from or to at least another one of the gas mixture, the liquid stream, the gas/vapor stream, gas-phase products and another flow in order to recycle energy.
  • the method also includes expanding and swirling the gas/vapor stream to produce first and second flows, wherein the first flow primarily includes heavy components of the gas/vapor stream and the second flow primarily includes lighter components of the gas/vapor stream; and transferring heat energy to or from at least one of the liquid stream, the gas/vapor stream, gas-phase products and the first and second flows from or to at least another one of the gas mixture, the liquid stream, the gas/vapor stream, gas-phase products, the another flow and the first and second flows in order to recycle energy.
  • the method also includes rectifying at least a portion of the first flow in conjunction with the liquid stream.
  • cooling the gas mixture includes at least partially mixing the gas mixture with at least a portion of at least one of the liquid stream, the gas/vapor stream, gas-phase products, the another flow and the first and second flows.
  • cooling the gas mixture includes at least partially transferring heat from the gas mixture to at least a portion of at least one of the liquid stream, the gas/vapor stream, gas-phase products, the another flow and the first and second flows.
  • the method also includes compressing at least a portion of the gas-phase products.
  • the method also includes cooling at least a portion the gas/vapor stream.
  • the method also includes compressing at least a portion of the first flow.
  • the method also includes compressing at least a portion of the second flow.
  • the method also includes cooling at least a portion of the first flow.
  • cooling at least a portion of the second flow.
  • the transfer of heat energy includes mixing at least a portion of the at least two streams or flows between which the heat is transferred.
  • the transfer of heat energy includes exchanging heat energy without mixing the at least two streams or flows between which the heat is transferred.
  • the method also includes passing at least a portion of the gas/vapor stream through a turbine.
  • the method also includes passing at least a portion of the second flow through a turbine.
  • the method also includes condensing at least a portion of the gas-phase products.
  • the method also includes further condensing at least a portion of the liquid stream.
  • the method also includes condensing at least a portion of the gas/vapor stream.
  • the method also includes expanding and swirling at least a portion of the gas-phase products.
  • a system for low-temperature gas mixture separation suitable for separating components of a hydrocarbon gas mixture, including: a first gas/liquid separator for separating an incoming gas mixture into a liquid stream and a gas/vapor stream; a first expander, for producing first and second flows, coupled the first gas/liquid separator to receive the gas/vapor stream, the first expander also including a swirling means for swirling the gas/vapor stream to thereby separate heavy components of the gas/vapor stream from the light components of the gas/vapor stream, wherein the heavy components primarily comprise the first flow and the lighter components primarily comprise the second flow; a rectifying tower, for producing at least gas-phase products, coupled to the first gas/liquid separator to receive the liquid stream; and at least one heat exchanger for transferring heat energy to or from at least one of the liquid stream, the gas/vapor stream, gas-phase products and the first and second flows from or to at least another one of the gas mixture, the liquid stream, the gas/vapor stream, gas-
  • the first expander is coupled to the rectifying tower to provide at least a portion of the first flow to the rectifying tower.
  • the system also includes a first mixer for mixing the incoming gas mixture with a feedback flow, the feedback flow comprising at least a portion of at least one the liquid stream, the gas/vapor stream, gas-phase products, the first and second flows and another flow.
  • system also includes a first compressor for compressing at least a portion of the gas-phase products.
  • system also includes a first compressor for compressing at least a portion of the gas/vapor stream.
  • system also includes a first compressor for compressing at least a portion of the first flow.
  • system also includes a first compressor for compressing at least a portion of the second flow.
  • system also includes a first chiller for cooling at least a portion of the first flow.
  • system also includes a first chiller for cooling at least a portion of the second flow.
  • the transfer of heat energy includes mixing at least a portion of the at least two streams or flows between which the heat is transferred.
  • the transfer of heat energy includes exchanging heat energy without mixing the at least two streams or flows between which the heat is transferred.
  • system also includes a turbine, for expanding at least a portion of the gas/vapor stream, coupled to the first gas/liquid separator to receive at least a portion of the gas/vapor stream.
  • system also includes a turbine through which at least a portion of the second flow passes, the turbine coupled to receive at least a portion of the second flow.
  • system also includes at least one other gas/liquid separator for separating at least one of a liquid or a gas/vapor stream within the system.
  • system also includes another condenser for further condensing at least a portion of the liquid stream.
  • system also includes another condenser for condensing at least a portion of the gas/vapor stream.
  • system also includes another expander for expanding and swirling at least a portion of the gas-phase products.
  • FIG. 1 is a schematic drawing of a low-temperature gas mixture separation system according to a first embodiment of the invention
  • FIG. 2 is a schematic drawing of a low-temperature gas separation apparatus shown in FIG. 1 ;
  • FIG. 3 is a schematic drawing of a low-temperature gas mixture separation system according to a second embodiment of the invention.
  • FIG. 4 is a schematic drawing of a low-temperature gas mixture separation system according to a third embodiment of the invention.
  • FIG. 5 is a schematic drawing of a low-temperature gas mixture separation system according to a fourth embodiment of the invention.
  • FIG. 6 is a schematic drawing of a low-temperature gas mixture separation system according to a fifth embodiment of the invention.
  • FIG. 7 is a schematic drawing of a low-temperature gas mixture separation system according to a sixth embodiment of the invention.
  • FIG. 8 is a schematic drawing of a low-temperature gas mixture separation system according to a seventh embodiment of the invention.
  • FIG. 9 is a schematic drawing of a low-temperature gas mixture separation system according to an eighth embodiment of the invention.
  • FIG. 10 is a schematic drawing of a low-temperature gas mixture separation system according to a ninth embodiment of the invention.
  • FIG. 11 is a schematic drawing of a low-temperature gas mixture separation system according to a tenth embodiment of the invention.
  • FIG. 12 is a schematic drawing of a low-temperature gas mixture separation system according to an eleventh embodiment of the invention.
  • FIG. 13 is a schematic drawing of a low-temperature gas mixture separation system according to a twelfth embodiment of the invention.
  • FIG. 14 is a schematic drawing of a low-temperature gas mixture separation system according to a thirteenth embodiment of the invention.
  • FIG. 15 is a schematic drawing of a low-temperature gas mixture separation system according to a fourteenth embodiment of the invention.
  • FIG. 16 is a schematic drawing of a low-temperature gas mixture separation system according to a fifteenth embodiment of the invention.
  • FIG. 17 is a schematic drawing of a low-temperature gas mixture separation system according to a sixteenth embodiment of the invention.
  • FIG. 18 is a schematic drawing of a low-temperature gas mixture separation system according to a seventeenth embodiment of the invention.
  • FIG. 19 is a schematic drawing of a low-temperature gas mixture separation system according to an eighteenth embodiment of the invention.
  • FIG. 20 is a schematic drawing of a low-temperature gas mixture separation system according to a nineteenth embodiment of the invention.
  • FIG. 21 is a schematic drawing of a low-temperature gas mixture separation system according to a twentieth embodiment of the invention.
  • FIG. 22 is a schematic drawing of a low-temperature gas mixture separation system according to a twenty-first embodiment of the invention.
  • FIG. 23 is a schematic drawing of a low-temperature gas mixture separation system according to a twenty-second embodiment of the invention.
  • some embodiments of the present invention provide a system for low-temperature gas mixture separation that recycles energy and reduces power consumption by re-circulating heated and/or cooled flows (e.g. gas, liquid and mixed-phase flows) within the system. Accordingly, in some embodiments efficiency is somewhat improved, as compared to comparable systems that do not include the re-circulation of heat energy.
  • the heat energy that is re-circulated is a combination of heat added to the system (i.e. inputs to the system) and heat released within the system (i.e. byproducts from within the system) that are subsequently recovered.
  • some systems and methods provided in accordance with embodiments of the invention are suited for separating the constituent components of natural gas and other hydrocarbon gas mixtures.
  • a method of low-temperate gas mixture separation includes expansion of a gas mixture without doing mechanical work (i.e. adiabatically expanding the gas mixture), which thereby cools and lowers the pressure of the gas mixture, a step that does not require an addition of energy into the system.
  • Expanding a gas mixture without doing mechanical work can be accomplished by passing the gas mixture through a Joules-Thompson valve or similar device having an expansion valve (or converging-diverging nozzle) that restricts the flow of gas entering an expansion chamber.
  • the gas mixture is also swirled as it enters the gas expanding apparatus.
  • the mixture flow is separated into at least two flows, a first flow that primarily includes the heavier components and a second flow that primarily includes the lighter components of the gas mixture.
  • the heavier components may also condense on the walls of the gas expanding apparatus, thereby facilitating an easier segregation of the first and second flows.
  • the first flow (primarily including the heavier components) is at least partially directed to a rectifying tower and the second flow is at least partially directed through a heat-exchanger in order to lower the temperature of an input gas mixture stream.
  • the gas-phase products produced in the rectifying tower are compressed, chilled and mixed with the input gas mixture before the input gas mixture arrives at the heat-exchanger.
  • the first flow is at least partially directed to a rectifying tower and the second flow is at least partially mixed with the gas-phase products produced in the rectifying tower. Additionally, in some embodiments the combination of the gas-phase products and the second flow are at least partially directed through a heat-exchanger in order to lower the temperature of an input gas mixture stream.
  • first flow is at least partially mixed with an input gas mixture stream, before the input gas mixture stream is expanded. Additionally, in some embodiments first flow is at least partially directed through a heat-exchanger in order to lower the temperature of an input gas mixture stream. In even more specific embodiments the first flow is also compressed and further chilled before being mixed with the input gas stream. In some such embodiments the second flow (i.e. the lighter flow) is outputted from the system alone or in a suitable combination with some gas-phase products produced elsewhere in the system.
  • FIG. 1 shown is a schematic drawing of a low-temperature gas mixture separation system 200 according to a first embodiment of the invention, referred to as the system 200 hereinafter for brevity.
  • the system 200 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 200 ; however, the system 200 is illustrated showing only those elements necessary to describe aspects of this embodiment.
  • the system 200 includes a first mixer 30 , a first heat-exchanger 32 , a first chiller 34 and a gas/liquid separator 36 connected respectively in series.
  • the first mixer 30 includes respective first and second inputs 30 a and 30 b .
  • the first input 30 a serves as an input to the system 200 as a whole as well as an input of the first mixer 30 .
  • the second input 30 b serves a feedback input, the purpose of which is described in more detail below.
  • the gas/liquid separator 36 has respective first and second outputs 36 a and 36 b .
  • the first output 36 a is a gas/vapor outlet and the second output 36 b is a liquid (or mixed-phase) output.
  • the gas/liquid separator 36 is a condenser.
  • the system also includes an expander 40 and a rectifying tower 38 .
  • the expander 40 is coupled to receive a gas/vapor flow from the first output 36 a of the gas/liquid separator 36 , whereas the second output 36 b of the gas/liquid separator 36 is coupled to deliver a liquid (or mixed-phase) flow to the rectifying tower 38 .
  • the expander 40 has respective first and second outputs 40 a and 40 b .
  • the first output 40 a is connected to deliver a first flow, of heavier components, to the rectifying tower 38 .
  • the second output 40 b is coupled back as an input to the first heat-exchanger 32 to cool the gas mixture entering by the first mixer 30 .
  • the rectifying tower 38 has respective first and second outputs 38 a and 38 b .
  • the first output 38 a is coupled back to the second input 30 b of the mixer 30 .
  • the system 200 also includes a compressor 42 and a second chiller 44 connected in series between the first output 38 a of the rectifying tower and the second input 30 b of the mixer 30 .
  • the expander 40 has a tubular body with an input end and an output end that are generally indicated by A and B, respectively.
  • the expander 40 includes a swirling means 41 near the input end and a converging-diverging nozzle section 43 following the swirling means 41 .
  • the swirling means 41 includes, without limitation, at least one of vanes, an impeller, and fins.
  • the converging-diverging nozzle section 43 flares open into a conical section 45 leading to the output end B.
  • a divider 47 is provided at the output end B within the conical section 45 to facilitate the separation of output flows leading to the respective first and second outputs 40 a and 40 b.
  • the expander 40 can be made both with flow swirling means placed at the nozzle channel entry as shown in FIG. 2 (e.g. as discussed in prior art references EP1131588 and U.S. Pat. No. 6,372,019) and with flow swirling means within the nozzle channel (e.g. as discussed in prior art references EP0496128 and WO99/01194).
  • the operation of the system 200 is as follows.
  • An incoming mixture 201 of natural gas (or another gas mixture) enters the system via the mixer 30 , where it is mixed with a feedback flow containing the compressed and cooled gas-phase products from the rectifying tower 38 .
  • the combination of the input natural gas and feedback gases is further cooled in the first heat-exchanger 32 .
  • the first heat-exchanger 32 facilitates the recycling of heat energy, or rather, in this particular case, the recycling of energy used to cool various flows within the system. That is, the first heat-exchanger 32 cools the incoming natural gas mixture by transferring heat from the natural gas mixture to a feedback flow originating from the second output 40 b of the expander 40 , which thereby lowers the temperature of the natural gas mixture.
  • the natural gas mixture is further cooled in the first chiller 34 before entering into the gas/liquid separator 36 .
  • the natural gas mixture is separated into a gas/vapor stream and a liquid (or mixed-phase) stream.
  • the gas/vapor stream flows out of the gas/liquid separator 36 via the first output 36 a directly into the expander 40 .
  • the liquid stream flows of the gas/liquid separator via the second output 36 b directly to the rectifying tower 38 .
  • the rectifying tower 38 outputs gas-phase products through the first output 38 a and liquid phase products through the second output 38 b .
  • the gas-phase products are compressed in the compressor 42 and cooled in the second chiller 44 before being mixed with the incoming mixture 201 as described above.
  • the incoming gas/vapor stream is separated into a first flow and a second flow.
  • the natural gas mixture enters the expander 40 , is swirled by the swirling means 41 , and expanded through the converging-diverging nozzle section 43 .
  • the swirling gas mixture expands the heavier components of the mixture drift away from a center axis around which the gas mixture is swirling while the lighter components remain near to the center axis.
  • the gas mixture flow is separated into at least the first and second flows, such that the first flow primarily includes the heavier components and the second flow primarily includes the lighter components.
  • the first flow exits the expander 40 through the first output 40 a .
  • the second flow exits the expander 40 through the second output 40 b.
  • the temperature of the gas/vapor stream is reduced enough to induce partial condensation of the mixture, thus forming a condensate.
  • the condensate drops in the field of centrifugal forces move toward the walls of the expander 40 collecting into a liquid (or two-phase) flow.
  • the gas mixture is natural gas the first flow contains components that are heavier than methane, whereas the second flow contains substantially more methane gas.
  • the static pressure of the mixture is lower than the pressure at the outputs of the expander 40 , and the mixture separation within the nozzle occurs at temperatures lower than the temperature of the mixture traveling through the outputs.
  • a deeper mixture separation is provided due to the gas-phase product from the rectifying tower 38 being fed back to the input mixture 201 before the mixture is processed further in the system 200 .
  • FIG. 3 shown is a schematic drawing of a low-temperature gas mixture separation system 300 according to a second embodiment of the invention, referred to as the system 300 hereinafter for brevity.
  • the system 300 illustrated in FIG. 3 is similar to the system 200 illustrated in FIG. 1 , and accordingly, elements common to both share common reference numerals. Moreover, for the sake of brevity, portions of the description of FIG. 1 will not be repeated with respect to FIG. 3 .
  • the system 300 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 300 ; however, the system 300 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the differences between the systems 200 and 300 are as follows.
  • the system 300 does not include the first mixer 30 , the first chiller 34 , the second chiller 44 and the first compressor 42 .
  • the system 300 does include a second mixer 48 and a first (throttling) valve 50 .
  • the first valve 50 is coupled between the second output 36 b of the gas/liquid separator 36 and the rectifying tower 38 .
  • the second mixer 48 includes respective first and second inputs that are coupled to receive and mix the gas/vapor outputs from the expander 40 and the rectifying tower 38 .
  • the second mixer 48 also includes an output that is coupled to deliver the gas mixture to the first heat-exchanger 32 .
  • the incoming mixture 301 is cooled in the first heat-exchanger 32 , before passing directly to the separator 36 .
  • the liquid stream from the separator 36 is then directed through the throttling valve 50 to the rectifying tower 38 .
  • the gas-phase products from the rectifying tower 38 are mixed with the second flow (primarily including the lighter components of the separation process) from the expander 40 in the second mixer 48 to produce a mixed feedback stream.
  • the mixed feedback stream is then passed through the first heat-exchanger 32 in which heat is transferred from the incoming mixture 301 to the feedback stream, thereby cooling the incoming mixture 301 without the addition of energy to the system 300 .
  • This method makes it possible to reduce required differential pressure of the mixture in the low temperature separation facilities.
  • FIG. 4 shown is a schematic drawing of a low-temperature gas mixture separation system 400 according to a third embodiment of the invention, referred to as the system 400 hereinafter for brevity.
  • the system 400 illustrated in FIG. 4 is similar to the respective systems illustrated in FIGS. 1 and 3 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 will not be repeated with respect to FIG. 4 .
  • the system 400 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 400 ; however, the system 400 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 400 are as follows.
  • the system 400 includes the first mixer 30 , as shown in FIG. 1 .
  • the system 400 also includes the second chiller 44 and the first compressor 42 .
  • the first compressor 42 and the second chiller 44 are connected between the first heat-exchanger 32 and the second input 30 b (i.e. the feedback input) of the first mixer 30 .
  • the first output 40 a of the expander 40 is coupled to the first heat-exchanger 32 instead of being coupled to the rectifying tower 38 as shown in FIG. 1 .
  • the incoming mixture 401 is mixed in the first mixer 30 with the first flow (i.e. the flow primarily including the heavier components of the mixture separated in the expander 40 ). That is, the first flow from the first output 40 a of the expander 40 is mixed with the incoming mixture 401 in order to cool the incoming mixture 401 .
  • the mixture outputted from the first mixer 30 is then passed through the first heat-exchanger 32 to further regulate the temperature of the incoming gas mixture.
  • the first heat-exchanger 32 is coupled to receive the first output 40 a of the expander 40 as a regulating inflow.
  • the gas-phase products output from the rectifying tower 38 are mixed with the second flow outputted from the second output 40 b of the expander 40 in the second mixer 48 and the combined mixture cannot be outputted from the system 400 .
  • FIG. 5 shown is a schematic drawing of a low-temperature gas mixture separation system 500 according to a fourth embodiment of the invention, referred to as the system 500 hereinafter for brevity.
  • the system 500 illustrated in FIG. 5 is similar to the respective systems illustrated in FIGS. 1 and 34 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 34 will not be repeated with respect to FIG. 5 .
  • the system 500 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 500 ; however, the system 500 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 500 are as follows.
  • the system 500 includes a second heat-exchanger 52 .
  • the second mixer 48 and the second heat-exchanger 52 are connected between the first output 36 a of the gas/liquid separator 36 and the input of the expander 40 .
  • the second heat-exchanger 52 is also coupled to receive the first flow from the first output 40 a of the expander 40 before the first flow is passed to the first heat-exchanger 32 , as described with respect to FIG. 4 .
  • the vapor stream from the separator 36 is mixed with the gas-phase output of the rectifying tower 38 in the second mixer 52 .
  • the output of the second mixer 48 is cooled in the second heat-exchanger 52 , before being passed through to the expander 40 .
  • the first flow (from the first output 40 a ) from the expander 40 is first sent through the second heat-exchanger 52 to cool the output of the second mixer 48 and then sent through the first heat-exchanger 32 to further cool the output of the first mixer 30 .
  • the same first flow is then compressed in compressor 42 , and is then cooled in a second chiller 44 before being mixed with the incoming gas mixture 501 .
  • the second flow (from the second output 40 b of the expander 40 ) can be directly output from the system 500 . By using the feedback system energy is again conserved and efficiency can be improved.
  • the system 500 facilitates a deep purification of the second flow output from the expander 40 (i.e. the flow primarily including lighter components of the gas mixture). That is, when considering the processing of natural gas the second flow may be significantly depleted of the vapor components heavier than methane, since the first flow is mixed with the incoming flow 501 .
  • FIG. 6 shown is a schematic drawing of a low-temperature gas mixture separation system 600 according to a fifth embodiment of the invention, referred to as the system 600 hereinafter for brevity.
  • the system 600 illustrated in FIG. 6 is similar to the respective systems illustrated in FIGS. 1 and 3 - 5 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 5 will not be repeated with respect to FIG. 6 .
  • system 600 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 600 ; however, the system 600 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 600 are as follows.
  • the system 600 includes a second gas/liquid separator 60 .
  • the second gas/liquid separator 60 includes respective first and second outputs 60 a and 60 b that are coupled to the second mixer 48 and the rectifying tower 38 , respectively.
  • the system 600 also includes a second (throttling valve 66 ) coupled between the second output 60 b and an input to the rectifying tower 38 .
  • the first output 40 a of the expander 40 is coupled to deliver the first flow from the expander 40 to the second gas/liquid separator 60 .
  • liquid separation in the form of condensation is performed twice: before and after various forms of the mixture are expanded in the expander 40 .
  • the first flow from the expander 40 is sent to a second separator 60 , which provides a second vapor stream and a second liquid stream.
  • the second liquid stream passes through a second throttling valve 66 and into the rectifying tower 38 .
  • a second vapor stream is mixed with the second flow from the expander 40 in the second mixer 48 .
  • the mixture 48 produced in the second mixer 48 is then passed through the first heat-exchanger 32 as described above.
  • FIG. 7 shown is a schematic drawing of a low-temperature gas mixture separation system 700 according to a sixth embodiment of the invention, referred to as the system 700 hereinafter for brevity.
  • the system 700 illustrated in FIG. 7 is similar to the respective systems illustrated in FIGS. 1 and 3 - 6 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 6 will not be repeated with respect to FIG. 7 .
  • system 700 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 700 ; however, the system 700 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 700 are as follows.
  • the second heat-exchanger 52 is coupled between the first throttling valve 50 and an input to the rectifying tower 38 .
  • the second chiller 44 is coupled between the rectifying tower 38 and the second heat-exchanger 52 . More specifically, the second chiller 44 is coupled to receive and cool the gas-phase products from the first output 36 a of the rectifying tower 38 .
  • the second heat-exchanger 52 is also coupled to the first mixer 30 to provide the cooled gas-phase products from the rectifying tower 38 as a feedback input to the first mixer 30 .
  • the incoming mixture 701 is mixed with the gas-phase products of the rectifying tower 38 as shown in FIG. 1 , however the gas-phase products are first cooled by the second chiller 44 and the second heat-exchanger 52 before mixing with the incoming mixture 701 .
  • the second heat-exchanger 52 heats the first flow (i.e. the heavy output flow) from the expander 40 before the first flow is delivered into the rectifying tower 38 .
  • This arrangement helps provide a more rational distribution of mass and enthalpy flows in the low-temperature separation process.
  • FIG. 8 shown is a schematic drawing of a low-temperature gas mixture separation system 800 according to a seventh embodiment of the invention, referred to as the system 800 hereinafter for brevity.
  • the system 800 illustrated in FIG. 8 is similar to the respective systems illustrated in FIGS. 1 and 3 - 7 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 7 will not be repeated with respect to FIG. 8 .
  • system 800 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 500 ; however, the system 800 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 800 are as follows. Liquid separation by condensation is facilitated twice before expansion in the expander 40 .
  • the second gas/liquid separator 60 is coupled to receive the combination of the liquid (or two phase output) from the first gas/liquid separator 36 and the gas-phase products from the rectifying tower 38 .
  • the gas-phase products from the rectifying tower 38 are first coupled through the second heat-exchanger 52 that also receives the liquid phase (or two phase) output of the second separator 60 , so that heat energy can be transferred between the two, thereby cooling one and heating the other in order to recycle energy within the system 800 .
  • the incoming mixture 801 is cooled in the first heat-exchanger 32 and further cooled in the first chiller 34 before entering the first gas/liquid separator 36 .
  • the liquid stream from the separator 36 is passed through a throttling valve 50 and is mixed with the gas-phase products of the rectifying tower 38 before entering the second gas/liquid separator 60 .
  • the second gas/liquid separator 60 also provides a second liquid stream, which passes through the second heat-exchanger 52 , thereby cooling the gas-phase products and heating the second liquid stream. After passing through the second heat-exchanger 52 the second liquid stream is coupled into the rectifying tower 38 .
  • the gas/vapor streams from the first and second separators 36 and 60 are combined in the second mixer 48 before being delivered to the expander 40 where the mixture undergoes the process above described with respect to FIGS. 1 and 2 to produce the first and second flows.
  • This method allows a deeper purification of the second flow by removing a greater proportion of components heavier than methane when natural gas is being processed.
  • FIG. 9 shown is a schematic drawing of a low-temperature gas mixture separation system 900 according to an eighth embodiment of the invention, referred to as the system 900 hereinafter for brevity.
  • the system 900 illustrated in FIG. 9 is similar to the respective systems illustrated in FIGS. 1 and 3 - 8 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 8 will not be repeated with respect to FIG. 9 .
  • system 900 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 900 ; however, the system 900 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 900 are as follows.
  • the first chiller 34 precedes the first heat-exchanger 32 .
  • a third heat-exchanger 62 is coupled in series between the first heat-exchanger 32 and the first gas/liquid separator 36 .
  • the third heat-exchanger 62 is also coupled to receive a portion of the liquid (or two phase) stream from the first gas/liquid separator 36 .
  • the second throttling valve 66 is coupled between the second output 36 b and the third heat-exchanger 62 to prevent a reversal of flow and maintain a forward pressure through the third heat-exchanger 62 .
  • the gas-phase products from the rectifying tower 38 are combined with the gas/vapor stream from the first gas/liquid separator 36 in the mixer 48 before expansion.
  • the second heat-exchanger 52 is coupled between the first output 38 a of the rectifying tower 38 and the second mixer 48 .
  • the second heat-exchanger 52 also receives a portion of the liquid stream from the first gas/liquid separator 36 , with the first throttling valve 50 connected there between.
  • a portion of the liquid stream from the first gas/liquid separator 36 is used to cool the incoming mixture 901 .
  • the incoming mixture 901 is cooled through the first chiller 34 and then is mixed with a portion of the liquid stream from the first gas/liquid separator 36 as described in more detail below.
  • the resulting mixture is further cooled in the first heat-exchanger 32 and in a third heat-exchanger 62 before entering the first gas/liquid separator 36 .
  • the first gas/liquid separator 36 produces a gas/vapor stream and a liquid (or two-phase) stream.
  • the gas/vapor stream is mixed in the second mixer 48 with the gas-phase products from the rectifying tower 38 , and the resulting gas/vapor mixture is expanded and separated into the first and second flows as described above with respect to FIGS. 1 and 2 .
  • the first flow is coupled into the rectifying tower 38 and the second flow is coupled back to the first heat-exchanger 32 .
  • the heat-exchangers facilitate the recycling of energy within the system 900 thereby improving the efficiency of the system 900 .
  • FIG. 10 shown is a schematic drawing of a low-temperature gas mixture separation system 1000 according ninth to a ninth embodiment of the invention, referred to as the system 1000 hereinafter for brevity.
  • the system 1000 illustrated in FIG. 10 is similar to the respective systems illustrated in FIGS. 1 and 3 - 9 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 9 will not be repeated with respect to FIG. 10 .
  • system 1000 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 1000 ; however, the system 1000 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 1000 are as follows.
  • the system 1000 includes a turbine 70 connected between the second output 40 b of the expander 40 and the first heat-exchanger 32 .
  • the addition of the turbine 70 effectively modifies the expander 40 to create a turbo-expander.
  • the system 1000 also includes a second compressor 64 connected in series between the first compressor 42 and the second input 30 b of the first mixer 30 .
  • the second flow coupled from the second output 40 b of the expander 40 , passes through the turbine 70 and is then sent back through the first heat-exchanger 32 to the incoming mixture 1001 .
  • a turbo-expander may be used to provide additional expansion, either before or after the mixture passes through the expander 40 .
  • the incoming mixture 1001 is mixed with a feed back gas/vapor stream that includes portions of the liquid stream of the first gas/liquid separator 36 and portions of the gas/vapor stream from the second gas/liquid separator 60 .
  • the resulting mixture is then cooled in the first heat-exchanger 32 before entering the first gas/liquid separator 36 .
  • the liquid stream of the first gas/liquid separator 36 is split into a first portion and a second portion.
  • the first portion passes through a throttling valve 50 and into the rectifying tower 58 .
  • the second portion of the first liquid stream is passed through a second throttling valve 66 before mixing with the gas/vapor stream of the second gas/liquid separator 60 .
  • the gas/vapor stream from the first gas/liquid separator 36 passes through the second heat-exchanger 52 where it is cooled before entering second mixer 48 .
  • the second mixer also receives the gas-phase products from the rectifying tower 38 .
  • the output of the second mixer 48 is then coupled into the expander 40 as described above.
  • the first flow from the expander 40 is directed into the second gas/liquid separator 60 .
  • the second separator 66 also provides the liquid stream which it produces directly to the rectifying tower 38 .
  • FIG. 11 shown is a schematic drawing of a low-temperature gas mixture separation system 1100 according to a tenth embodiment of the invention, referred to as the system 1100 hereinafter for brevity.
  • the system 1100 illustrated in FIG. 11 is similar to the respective systems illustrated in FIGS. 1 and 3 - 10 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 10 will not be repeated with respect to FIG. 11 .
  • system 900 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 1100 ; however, the system 1100 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the first input 30 a to the first mixer 30 serves as an input to the system 1100 as well as an input to the first mixer 30 .
  • the first compressor 42 is coupled in series between the first mixer 30 and the first chiller 34 , which is in turn coupled in series to the first heat-exchanger 32 .
  • the first and second outputs of the first heat-exchanger 32 are connected to the first gas/liquid separator 36 and the second compressor 64 respectively.
  • the second output 36 b of the first gas/liquid separator 36 is coupled to the parallel combination of first and second throttling vales 50 and 66 , which are in turn connected to the rectifying tower 38 and the second heat-exchanger 52 , respectively.
  • the liquid (two-phase) stream from the first gas/liquid separator is divided between the second heat-exchanger 52 and the rectifying tower.
  • the second heat-exchanger 52 is also coupled to receive the gas/vapor stream output of the first gas/liquid separator before the gas/vapor stream enters the expander.
  • the system 1100 is particularly useful when, in operation, the incoming mixture 1101 enters at a relatively low differential pressure. More specifically, the incoming mixture 1101 is mixed with the second flow separated in the expander 40 . The resulting combined mixture is then compressed in a first compressor 42 before being cooled in the first chiller 34 and the first heat-exchanger 32 .
  • the liquid stream from the first gas/liquid separator 36 is split into a first portion, which passes through a first throttling valve 50 into the rectifying tower 38 , and a second portion that passes through the second throttling valve 66 into the second heat-exchanger 52 .
  • the second portion After traveling through the second heat-exchanger 52 , the second portion enters the second mixer 48 , where it is mixed with the gas-phase products of the rectifying tower 38 .
  • the combination is then fed back to the first mixer 30 to be mixed with the incoming mixture 1101 , as described above.
  • the gas/vapor stream 36 from the first separator is sent to the expander 40 and undergoes the process described above with respect to FIGS. 1 and 2 .
  • FIG. 12 shown is a schematic drawing of a low-temperature gas mixture separation system 1200 according to an eleventh embodiment of the invention, referred to as the system 1200 hereinafter for brevity.
  • the system 1200 illustrated in FIG. 12 is similar to the respective systems illustrated in FIGS. 1 and 3 - 11 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 11 will not be repeated with respect to FIG. 12 .
  • system 1200 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 1200 ; however, the system 1200 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 1200 are as follows.
  • the gas/vapor stream of the first gas/liquid separator 36 is split into two streams.
  • the first stream is coupled into the expander 40 .
  • the second stream is coupled into the turbine 70 that is placed in parallel with the expander 40 .
  • the first output 40 a of the expander 40 and the output of the turbine 70 meet at the second mixer 48 that is in turn coupled to the rectifying tower 38 .
  • the second output 40 b of the expander 40 and the first output 38 a of the rectifying tower meet at the third mixer 68 that is in turn connected in series to the second heat-exchanger 52 and the second compressor 64 .
  • the system 1200 is suitable for situations in which it is desirable to provide increased pressure within the system to improve the effectiveness of the mixture separation.
  • the resulting mixture is compressed in the compressor 42 and cooled in the first chiller 34 and the first heat-exchanger 32 .
  • Another portion of the liquid stream from the first gas/liquid separator 36 is passed through the throttling valve 50 and into the rectifying tower 38 .
  • the gas/vapor stream of the first gas/liquid separator 36 is also split into two portions. The first portion is directed into the turbine 70 and the second portion is directed into the expander 40 .
  • the first flow from the expander 40 and the output of the turbine 70 are mixed and delivered to the rectifying tower 38 .
  • the second flow is mixed with the gas-phase products from the rectifying tower 38 and passes through the second heat-exchanger 52 and compressor 64 before exiting the system.
  • FIG. 13 shown is a schematic drawing of a low-temperature gas mixture separation system 1300 according to a twelfth embodiment of the invention, referred to as the system 1300 hereinafter for brevity.
  • the system 1300 illustrated in FIG. 13 is similar to the respective systems illustrated in FIGS. 1 and 3 - 12 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 12 will not be repeated with respect to FIG. 13 .
  • system 1300 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 1300 ; however, the system 1300 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 1300 are as follows.
  • the system 1300 includes a second expander 80 similar in design and function to the expander 40 described above with respect to FIG. 2 .
  • the expander 80 Analogous to the first expander 40 , the expander 80 has respective first and second outputs 80 a and 80 b .
  • the first output 80 a is connected to deliver a first flow, of heavier components, to the second gas/liquid separator 60
  • the second output 40 b is coupled to combine a second flow, of lighter components, with the gas/vapor stream of the second gas/liquid separator 60 .
  • the system 1300 also includes a pump 72 and a third throttling valve 74 connected in series between the liquid (or two-phase) stream (i.e.
  • the second output 60 b of the second gas/liquid separator 60 and the third heat-exchanger 62 which is in turn coupled to the rectifying tower 38 .
  • the gas-phase products from the rectifying tower 38 are also coupled through the third heat-exchanger 62 .
  • the gas-phase products from the rectifying tower 38 are cooled, expanded (in the second expander 80 ) and separated, and the resulting second flow from the second expander 80 is directed, either partially or totally, back to the rectifying tower 38 .
  • FIG. 14 shown is a schematic drawing of a low-temperature gas mixture separation system 1400 according to a thirteenth embodiment of the invention, referred to as the system 1400 hereinafter for brevity.
  • the system 1400 illustrated in FIG. 14 is similar to the respective systems illustrated in FIGS. 1 and 3 - 13 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 13 will not be repeated with respect to FIG. 14 .
  • system 1400 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 1400 ; however, the system 1400 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 1400 are as follows.
  • the system 1400 includes a cooling and compression loop connected between the first output 38 a of the rectifying tower 38 and the input of the second gas/liquid separator 60 that includes a third heat-exchanger 76 , the second compressor 64 and second chiller 44 connected in series.
  • the output of the second chiller 44 is then connected in a feedback loop through the third heat-exchanger 76 .
  • the first output 60 a i.e. the gas/vapor output
  • the first output 80 a (containing the heavier of the separated components from the expansion and separation process) of the expander 80 is coupled to the rectifying tower 38 and the second output 80 b is combined with the second output 40 b of the expander 40 .
  • the gas-phase products from the rectifying tower 38 are chilled and compressed in the aforementioned cooling and compression loop. Specifically, the gas-phase products from the rectifying tower 38 are cooled in the heat-exchanger 76 , compressed in the compressor 64 , cooled in the chiller 44 , and further cooled in second heat-exchanger 62 before entering into the second gas/liquid separator 60 . The liquid stream from the second gas/liquid separator 60 also passes through the second heat-exchanger 162 before entering into the rectifying tower 38 .
  • the operation of the rest of the system 1400 is analogous to that of the system 1300 illustrated in FIG. 13 .
  • FIG. 15 shown is a schematic drawing of a low-temperature gas mixture separation system 1500 according to a fourteenth embodiment of the invention, referred to as the system 1500 hereinafter for brevity.
  • the system 1500 illustrated in FIG. 15 is similar to the respective systems illustrated in FIGS. 1 and 3 - 14 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 14 will not be repeated with respect to FIG. 15 .
  • system 1500 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 1500 ; however, the system 1500 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • system 1500 the first output 38 a of the rectifying tower 38 is coupled to the input of second expander 80 via the second chiller 44 .
  • the first output 80 a of the expander 80 is coupled to the second gas/liquid separator 60 .
  • the liquid (or two-phase) output of the separator 60 is coupled into the rectifying tower 38 .
  • the gas-phase products from the rectifying tower 38 are expanded within the second expander 80 to separate heavy and light components from one another as described above with respect to FIG. 2 .
  • the first flow (containing the heavier components) from the first output 80 a of the second expander 80 passes into the second gas/liquid separator 60 .
  • the liquid (or two-phase) output is pumped into the rectifying tower 38 through pump 72 and the third throttling valve 74 .
  • the second output 80 b of the expander 80 is combined with the gas/vapor stream output from the second separator 60 and the second output 40 b of the expander 40 .
  • the resulting mixture is fed back to the first heat-exchanger 32 to cool the incoming mixture 1501 .
  • the incoming mixture 1501 having been mixed with a feedback flow as described previously, is also compressed before entering the first gas/liquid separator 36 .
  • the remaining operations are similar to the systems described previously.
  • FIG. 16 shown is a schematic drawing of a low-temperature gas mixture separation system 1600 according to a fifteenth embodiment of the invention, referred to as the system 1600 hereinafter for brevity.
  • the system 1600 illustrated in FIG. 16 is similar to the respective systems illustrated in FIGS. 1 and 3 - 15 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 15 will not be repeated with respect to FIG. 16 .
  • system 1600 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 1600 ; however, the system 1600 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the system 1600 only includes the first gas/liquid separator 36 .
  • the third heat-exchanger 62 is connected in series between the first output 38 a of the rectifying tower 38 and the input of the second expander 80 .
  • the first output 80 a of the expander 80 is fed back and coupled through the third heat-exchanger 62 via the third throttling valve 74 and through the second heat-exchanger 52 , which is in turn coupled back to the first mixer 30
  • the first flow separated in the second expander 80 travels through the third and second heat-exchangers 62 and 52 , respectively before being combined with the incoming mixture 1601 .
  • the liquid (or two-phase) output stream from the first gas/liquid separator 36 is also combined with the first flow separated in the second expander 80 before the second heat-exchanger 52 .
  • the second throttling valve 66 prevents back flow of the liquid output stream to the first gas/liquid separator 36 .
  • the remaining elements operate as discussed with respect to FIG. 15 .
  • FIG. 17 shown is a schematic drawing of a low-temperature gas mixture separation system 1700 according to a sixteenth embodiment of the invention, referred to as the system 1700 hereinafter for brevity.
  • the system 1700 illustrated in FIG. 17 is similar to the respective systems illustrated in FIGS. 1 and 3 - 16 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 16 will not be repeated with respect to FIG. 17 .
  • system 1700 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 1700 ; however, the system 1700 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 1700 are as follows.
  • the system 1700 includes four gas/liquid separators, namely, the first and second gas/liquid separators 36 and 60 and additionally third and fourth gas/liquid separators 82 and 84 .
  • the first and second gas/liquid separators 36 and 60 are connected such that the gas/vapor output of the first gas/liquid separator 36 is coupled into the second gas/liquid separator 60 .
  • the turbine 70 and second mixer 48 are connected there between, as illustrated in FIG. 17 .
  • the liquid outputs of the first and second gas/liquid separators 36 and 60 are combined and coupled to the third separator 82 .
  • the liquid output of the third separator 82 is coupled to the fourth separator 84 via the second heat-exchanger 52 .
  • the liquid output of the fourth gas/liquid separator 84 is coupled to the rectifying tower 38 and the gas/vapor output is coupled through the second mixer 48 to the second gas/liquid separator 60 along with the gas/vapor output of the third gas/liquid separator 82 .
  • the gas/vapor output stream of the second gas/liquid separator 60 is coupled into the expander 40 .
  • the compressor stage of the turbo-expander can be used as compressor 42 , and this scheme makes it possible to improve power consumption in the process of low-temperature separation.
  • the incoming mixture 1701 is cooled by the series combination of the first and second heat-exchangers 32 and 52 before entering the first gas/liquid separator 36 .
  • the liquid streams from the first and second gas/liquid separator 36 , 60 are combined and directed into the third gas/liquid separator 82 along with the first flow produce by the expander 40 .
  • the third gas/liquid separator 82 produces a liquid stream that is used as a coolant in the second heat-exchanger 52 before being further processed in the fourth gas/liquid separator 84 .
  • the liquid stream produced by the fourth gas/liquid separator 84 is then delivered to the rectifying tower 38 .
  • the gas/vapor streams from the third and fourth gas/liquid separators 82 and 84 are combined and fed back to the second gas/liquid separator 60 along with the gas/vapor stream from the first gas/liquid separator.
  • FIG. 18 shown is a schematic drawing of a low-temperature gas mixture separation system 1800 according to a seventeenth embodiment of the invention, referred to as the system 1800 hereinafter for brevity.
  • the system 1800 illustrated in FIG. 18 is similar to the respective systems illustrated in FIGS. 1 and 3 - 17 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 17 will not be repeated with respect to FIG. 18 .
  • system 1800 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 1800 ; however, the system 1800 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 1800 are as follows.
  • the liquid stream output 36 b of the first gas/liquid separator 36 is coupled to both the rectifying tower 38 and the third heat-exchanger 62 .
  • the third heat-exchanger 62 is coupled in series between the first heat-exchanger 32 and the first gas/liquid separator 36 .
  • the third heat exchange 62 couples the liquid stream output 36 b back to the first mixer 30 via the first compressor 42 and the second chiller 44 .
  • a portion of the liquid stream from the first gas/liquid separator 36 is used to cool the incoming mixture 1701 , as shown by example in FIG. 18 .
  • the incoming mixture 1701 is cooled through the first chiller 34 and then mixed with a portion of the liquid stream from the first gas/liquid separator 36 . That portion of the liquid stream, however, is first used as a coolant in the third heat-exchanger 62 and then compressed and chilled before being added to the incoming mixture 1701 .
  • the remaining portions of the system operate as described with respect to FIG. 3 .
  • FIG. 19 shown is a schematic drawing of a low-temperature gas mixture separation system 1900 according to an eighteenth embodiment of the invention, referred to as the system 1900 hereinafter for brevity.
  • the system 1900 illustrated in FIG. 19 is similar to the respective systems illustrated in FIGS. 1 and 3 - 18 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 18 will not be repeated with respect to FIG. 19 .
  • system 1900 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 1900 ; however, the system 1900 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 1900 are as follows.
  • the gas/vapor stream of the first gas/liquid separator 36 is split into two streams.
  • the first stream is coupled into the expander 40 .
  • the second stream is coupled into the turbine 70 that is placed in parallel with the expander 40 .
  • the first output 40 a of the expander 40 and the output of the turbine 70 are coupled into the rectifying tower 38 .
  • the second output 40 b of the expander 40 and the first output 38 a of the rectifying tower meet at the second mixer 48 that is in turn connected in series to the first heat-exchanger 32 .
  • the system 1900 is suitable for situations in which it is desirable to provide increased pressure within the system to improve the effectiveness of the mixture separation.
  • incoming mixture 1901 is cooled in the first heat-exchanger 32 and separated in the first gas/liquid separator 36 .
  • the liquid stream 16 passes through a valve 42 and into the rectifying tower 18 .
  • the gas/vapor stream produced by the first gas/liquid separator 36 is separated into at least two flows, one of which is pumped through a turbo-expander turbine 70 and directed to the rectifying tower 38 , and the other flow is expanded through the expander 40 .
  • the first flow from the expander 40 is sent to the rectifying tower 38
  • the second flow is mixed with the gas-phase products from the rectifying tower 38 , the combination of which is sent through the first heat-exchanger 32 and outputted after being compressed in the first compressor 42 .
  • This method is applicable for deeper purification of the mixture and for substantially removing heavier components from the mixture.
  • FIG. 20 shown is a schematic drawing of a low-temperature gas mixture separation system 2000 according to a nineteenth embodiment of the invention, referred to as the system 2000 hereinafter for brevity.
  • the system 2000 illustrated in FIG. 20 is similar to the respective systems illustrated in FIGS. 1 and 3 - 19 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 19 will not be repeated with respect to FIG. 20 .
  • system 2000 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 2000 ; however, the system 2000 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 2000 are as follows.
  • the system 2000 is almost identical to the system 1900 with the exception that the compressor 42 is not included.
  • this system 2000 may facilitates improved efficiency of the turbo-expander turbine 70 , thus providing for deeper gas cooling in the turbine 70 and allowing for a greater compression ratio.
  • FIG. 21 shown is a schematic drawing of a low-temperature gas mixture separation system 2100 according to a twentieth embodiment of the invention, referred to as the system 2100 hereinafter for brevity.
  • the system 2000 illustrated in FIG. 21 is similar to the respective systems illustrated in FIGS. 1 and 3 - 20 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 20 will not be repeated with respect to FIG. 20 .
  • system 2100 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 2100 ; however, the system 2100 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 2100 are as follows.
  • the first output 36 a of the first gas/liquid separator 36 is split between the turbine 70 , the expander 40 and the third mixer 68 .
  • the third mixer 68 also receives the first flow from the expander 40 and the gas-phase products from the rectifying tower 38 .
  • the gas/vapor stream produced by the first separator 36 is divided into three portions that are passed to the turbine 70 , the expander 40 and the third mixer 68 , respectively.
  • the remaining components operate as discussed with reference to FIGS. 19 and 20 .
  • This method makes it possible to stabilize the mass flow rate through the turbo-expander turbine 70 in case of variations in the incoming mixture 2101 .
  • FIG. 22 shown is a schematic drawing of a low-temperature gas mixture separation system 2200 according to a twenty-first embodiment of the invention, referred to as the system 2200 hereinafter for brevity.
  • the system 2200 illustrated in FIG. 15 is similar to the respective systems illustrated in FIGS. 1 and 3 - 21 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 21 will not be repeated with respect to FIG. 22 .
  • system 2200 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 2200 ; however, the system 2200 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 2200 are as follows.
  • the second output (i.e. the liquid output) 36 b of the first gas/liquid separator and the first output 40 a of the expander 40 are coupled into the second mixer 48 , which is in turn coupled to the first heat-exchanger 32 .
  • the resulting combination of the liquid output of the first gas/liquid separator 26 and the first flow from the expander 40 is used to cool the incoming mixture 2201 within the first heat-exchanger 32 , as well as being added to the incoming mixture 2201 within the first mixer 30 .
  • This method can be effective in cases where the gas-phase products produced by the rectifying tower 38 contain relatively light components from the incoming mixture 2201 .
  • the gas-phase products produced by the rectifying tower 38 may have very low amounts of components that are heavier than methane.
  • FIG. 23 shown is a schematic drawing of a low-temperature gas mixture separation system 2300 according to a twenty-second embodiment of the invention, referred to as the system 2300 hereinafter for brevity.
  • the system 2300 illustrated in FIG. 23 is similar to the respective systems illustrated in FIGS. 1 and 3 - 22 , and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for FIGS. 1 and 3 - 22 will not be repeated with respect to FIG. 23 .
  • system 2300 includes a suitable combination of associated structural elements, mechanical systems, hardware, firmware and software that is employed to support the function and operation of the system 2300 ; however, the system 2300 is illustrated showing only those elements necessary to describe aspects of this embodiment of the invention.
  • the arrangements specifically shown with respect to the system 2300 are as follows. A portion of the second output 36 b of the first gas/liquid separator 36 and the first output 40 a of the expander 40 are connected and coupled through the second and the third heat-exchangers 52 and 62 . The first output 38 a of the rectifying tower 38 is also coupled with the corresponding output of the third heat-exchanger 62 and then coupled into the first compressor 42 . The first compressor 42 is then coupled in series to through the second chiller 44 to the first mixer 30 that also accepts the incoming mixture 2301 .
  • a portion of the liquid output from the first gas/liquid separator 36 is combined with the first flow produced by the expander 40 .
  • the combination is used to chill the gas/vapor stream from the first gas/liquid separator 36 in the second heat-exchanger 52 and the incoming mixture 2301 in the third heat-exchanger 62 before being combined with the incoming mixture 2301 in the mixer 30 .
  • the system 2300 is suitable for processing gas mixtures in which the concentration of the target components is low in the incoming mixture.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
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  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Separation Of Gases By Adsorption (AREA)
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BRPI0516049B1 (pt) 2018-11-27
BRPI0516049A (pt) 2008-08-19
CN101069055A (zh) 2007-11-07
EA010564B1 (ru) 2008-10-30
CA2520800C (fr) 2014-08-19
AU2005287826A1 (en) 2006-03-30
CN101069055B (zh) 2010-06-23
GB2432413B (en) 2008-04-16
GB0705692D0 (en) 2007-05-02
RU2272973C1 (ru) 2006-03-27
AU2005287826B2 (en) 2010-12-16
NO20071943L (no) 2007-06-14
EA200700625A1 (ru) 2007-10-26
WO2006032139A1 (fr) 2006-03-30
CA2520800A1 (fr) 2006-03-24
GB2432413A (en) 2007-05-23

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