WO2006032139A1 - 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
WO2006032139A1
WO2006032139A1 PCT/CA2005/001437 CA2005001437W WO2006032139A1 WO 2006032139 A1 WO2006032139 A1 WO 2006032139A1 CA 2005001437 W CA2005001437 W CA 2005001437W WO 2006032139 A1 WO2006032139 A1 WO 2006032139A1
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WO
WIPO (PCT)
Prior art keywords
mixture
expansion
gas
rectifying tower
products
Prior art date
Application number
PCT/CA2005/001437
Other languages
English (en)
French (fr)
Inventor
Vadim Ivanovich Alferov
Lev Arkad'evich Bagirov
Vladimir Isaakovich Feygin
Salavat Zainetdinovich Imaev
Leonard Makarovich Dmitriev
Original Assignee
Translang Technologies Ltd.
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Translang Technologies Ltd. filed Critical Translang Technologies Ltd.
Priority to MX2007003514A priority Critical patent/MX2007003514A/es
Priority to BRPI0516049A priority patent/BRPI0516049B1/pt
Priority to GB0705692A priority patent/GB2432413B/en
Priority to CN2005800402687A priority patent/CN101069055B/zh
Priority to AU2005287826A priority patent/AU2005287826B2/en
Priority to EA200700625A priority patent/EA010564B1/ru
Publication of WO2006032139A1 publication Critical patent/WO2006032139A1/en
Priority to NO20071943A priority patent/NO20071943L/no

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Classifications

    • 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.
  • Patent US6182468B1 The typical processes of low temperature separation of the aimed components from the gas mixtures are described, for example, in the Patents US6182468B1 and RU2047061C1.
  • the method of Patent US6182468B1 is based on the gas chilling at the expense of gas mixture throttling in Joule-Thompson valve while in the Patent RU2047061C1 the turbo expander turbine is used for the gas chilling.
  • Patent US6182468B1 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 cooling of the 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
  • the process of the mixture expansion is implemented by passing the mixture through the nozzle channel such that in the nozzle channel and/or at the entry of the nozzle channel the mixture flow is swirled, at the exit of the nozzle channel or its part the mixture flow is separated into, at least, two flows, one of which is enriched in components heavier than methane, while the other flow is depleted in these components; the enriched flow is directed, either partially or totally, to the rectifying tower, and the gas-phase products, obtained in the rectifying tower, are directed, either partially or totally, to the mixture before its expansion.
  • 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. [0016] In some more specific embodiments 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. [0025] In some more specific embodiments 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. [0027] In some more specific embodiments 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
  • 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.
  • the 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.
  • an enriched flow is directed, either partially or totally, to the rectifying tower, and the gas-phase products, coming from the rectifying tower, are mixed, either partially or totally, with a depleted flow; the enriched flow is directed, either partially or totally, to the mixture before its expansion, and the gas-phase products, coming from the rectifying tower, are mixed, either partially or totally, with the depleted flow; and the enriched flow and the gas-phase products, coming from the rectifying tower, are directed, either partially or totally, to the mixture before its expansion.
  • FIG. 1 is a schematic drawing of a low-temperature gas mixture separation system according to a first embodiment of the invention
  • Figure 2 is a schematic drawing of a low-temperature gas separation apparatus shown in Figure 1;
  • Figure 3 is a schematic drawing of a low-temperature gas mixture separation system according to a second embodiment of the invention;
  • Figure 4 is a schematic drawing of a low-temperature gas mixture separation system according to a third embodiment of the invention.
  • Figure 5 is a schematic drawing of a low-temperature gas mixture separation system according to a fourth embodiment of the invention.
  • Figure 6 is a schematic drawing of a low-temperature gas mixture separation system according to a fifth embodiment of the invention.
  • Figure 7 is a schematic drawing of a low-temperature gas mixture separation system according to a sixth embodiment of the invention.
  • Figure 8 is a schematic drawing of a low-temperature gas mixture separation system according to a seventh embodiment of the invention.
  • Figure 9 is a schematic drawing of a low-temperature gas mixture separation system according to an eighth embodiment of the invention.
  • Figure 10 is a schematic drawing of a low-temperature gas mixture separation system according to a ninth embodiment of the invention.
  • Figure 11 is a schematic drawing of a low-temperature gas mixture separation system according to a tenth embodiment of the invention.
  • Figure 12 is a schematic drawing of a low-temperature gas mixture separation system according to an eleventh embodiment of the invention.
  • Figure 13 is a schematic drawing of a low-temperature gas mixture separation system according to a twelfth embodiment of the invention.
  • Figure 14 is a schematic drawing of a low-temperature gas mixture separation system according to a thirteenth embodiment of the invention.
  • Figure 15 is a schematic drawing of a low-temperature gas mixture separation system according to a fourteenth embodiment of the invention.
  • Figure 16 is a schematic drawing of a low-temperature gas mixture separation system according to a fifteenth embodiment of the invention.
  • Figure 17 is a schematic drawing of a low-temperature gas mixture separation system according to a sixteenth embodiment of the invention.
  • Figure 18 is a schematic drawing of a low-temperature gas mixture separation system according to a seventeenth embodiment of the invention.
  • Figure 19 is a schematic drawing of a low-temperature gas mixture separation system according to an eighteenth embodiment of the invention.
  • Figure 20 is a schematic drawing of a low-temperature gas mixture separation system according to a nineteenth embodiment of the invention.
  • Figure 21 is a schematic drawing of a low-temperature gas mixture separation system according to a twentieth embodiment of the invention.
  • Figure 22 is a schematic drawing of a low-temperature gas mixture separation system according to a twenty-first embodiment of the invention.
  • Figure 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 invention may enable reduced power consumption in the LTS facilities. To that end, in accordance with some embodiments of the invention, this may be accomplished in the first embodiment of the present method owing to the fact that in the known LTS process for a mixture of hydrocarbon gases, which includes cooling of the mixture, expansion of the mixture or its part 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 products in liquid and gas phase, in accordance with the present invention, the process of mixture expansion is implemented by passing the mixture through the nozzle channel such that in the nozzle channel and/or at the entry of the nozzle channel the mixture flow is swirled, and at the exit of the nozzle channel or its part the mixture flow is separated into, at least, two flows, one of which is enriched in components heavier than methane, while the other flow is depleted in these components, and the enriched flow is directed, either partially or totally, to the rectifying tower, and the gas-phase products, obtained in the rectifying tower, and the gas-phase products
  • 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
  • the first mixer 30 includes respective first and second inputs 30a and 30b.
  • the first input 30a serves as an input to the system 200 as a whole as well as an input of the first mixer 30.
  • the second input 30b 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 36a and 36b.
  • the first output 36a is a gas/vapor outlet and the second output 36b is a liquid (or mixed-phase) output.
  • the gas/liquid separator 36 is a condenser.
  • the system also includes a device for expansion of the mixture
  • the device for expansion of the mixture 40 is coupled to receive a gas/vapor flow from the first output 36a of the gas/liquid separator 36, whereas the second output 36b of the gas/liquid separator 36 is coupled to deliver a liquid (or mixed-phase) flow to the rectifying tower 38.
  • the device for expansion of the mixture 40 has respective first and second outputs 40a and 40b.
  • the first output 40a is connected to deliver a first flow, primarily containing heavier components, to the rectifying tower 38.
  • the second output 40b is coupled back as an input to the first heat- exchanger 32 to cool the gas mixture entering first mixer 30.
  • the rectifying tower 38 has respective first and second outputs
  • the system 200 also includes a compressor 42 and a second chiller 44 connected in series between the first output 38a of the rectifying tower and the second input 30b of the mixer 30.
  • the device for expansion of the mixture 40 has a tubular body with an input end and an output end that are generally indicated by A and B, respectively.
  • the device for expansion of the mixture 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.
  • 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 40a and 40b.
  • the device for expansion of the mixture 40 can be made both with flow swirling means placed at the nozzle channel entry as shown in Figure 2 (e.g. as discussed in prior art references EP1131588 and US6372019) and with flow swirling means within the nozzle channel (e.g. as discussed in prior art references EP0496128 and WO99/01194).
  • An incoming mixture 201 of natural gas 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 40b of the device for expansion of the mixture 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 36a directly into the device for expansion of the mixture 40.
  • the liquid stream flows of the gas/liquid separator via the second output 36b directly to the rectifying tower 38.
  • the rectifying tower 38 outputs gas-phase products through the first output 38a and liquid phase products through the second output 38b.
  • 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 device for expansion of the mixture 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 while the lighter components remain near to the center axis. That is why 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 device for expansion of the mixture 40 through the first output 40a.
  • the second flow exits the device for expansion of the mixture 40 through the second output 40b.
  • 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 device for expansion of the mixture 40 collecting into a two-phase flow near the wall.
  • 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 device for expansion of the mixture 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. 2 demonstrates an example when in the device for the mixture expansion at the exit of the nozzle channel the mixture flow is separated into two flows, and then each flow is compressed in the diffuser. This allows to reduce pressure losses on the expanding device.
  • the process of the mixture expansion is implemented by passing the mixture through the nozzle channel such that in the nozzle channel and /or at the entry of the nozzle channel the mixture flow is swirled, at the exit of the nozzle channel or its part the mixture flow is separated into, at least, two flows, one of which is enriched in components heavier than methane, while the other flow is depleted in these components, and the enriched flow is directed, either partially or totally, to the rectifying tower, while the gas-phase products, coming from the rectifying tower, are mixed, either partially or totally, with the depleted flow.
  • 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 Figure 3 is similar to the system 200 illustrated in Figure 1 , and accordingly, elements common to both share common reference numerals. Moreover, for the sake of brevity, portions of the description of Figure 1 will not be repeated with respect to Figure 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 36b 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 device for expansion of the mixture 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 device for expansion of the mixture 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.
  • the process of the mixture expansion is implemented by passing the mixture through the nozzle channel such that in the nozzle channel and/or at the entry of the nozzle channel the mixture flow is swirled, at the exit of the nozzle channel or its part the mixture flow is separated into, at least, two flows, one of which is enriched in components heavier than methane, while the other is depleted in these components, and the enriched flow is directed, either partially or totally, to the mixture before its expansion, and the gas-phase products, coming from the rectifying tower, are mixed, either partially or totally, with the depleted flow.
  • 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 Figure 4 is similar to the respective systems illustrated in Figures 1 and 3, and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for Figures 1 and 3 will not be repeated with respect to Figure 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 system 400 includes the first mixer 30, as shown in Figure 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 30b (i.e. the feedback input) of the first mixer 30.
  • the first output 40a of the device for expansion of the mixture 40 is coupled to the first heat- exchanger 32 instead of being coupled to the rectifying tower 38 as shown in Figure 1.
  • the first flow i.e. the flow primarily including the heavier components of the mixture separated in the device for expansion of the mixture 40. That is, the first flow from the first output 40a of the device for expansion of the mixture 40 is mixed with 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 40a of the device for expansion of the mixture 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 40b of the device for expansion of the mixture 40 in the second mixer 48 and the combined mixture cannot be outputted from the system 400.
  • the process of the mixture expansion is implemented by passing the mixture through the nozzle channel such that in the nozzle channel and/or at the entry of the nozzle channel the mixture flow is swirled, at the exit of the nozzle channel or its part the mixture flow is separated into, at least, two flows, one of which is enriched with components heavier than methane, while the other flow is depleted in these components, and the enriched flow and gas-phase products, coming from the rectifying tower, are directed, either partially or totally, to the mixture before its expansion.
  • 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 Figure 5 is similar to the respective systems illustrated in Figures 1 and 3-4, and accordingly, elements common to each share common reference numerals. Moreover, for the sake of brevity, portions of the descriptions for Figure 1 and 3-4 will not be repeated with respect to Figure 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 system 500 includes a second heat-exchanger 52.
  • the second mixer 48 and the second heat-exchanger 52 are connected between the first output 36a of the gas/liquid separator 36 and the input of the device for expansion of the mixture 40.
  • the second heat-exchanger 52 is also coupled to receive the first flow from the first output 40a of the device for expansion of the mixture 40 before the first flow is passed to the first heat- exchanger 32, as described with respect to Figure 4.
  • the vapor stream from the separator 36 is mixed with the gas-phase output of the rectifying tower 38 in the second mixer 48.
  • the output of the second mixer 48 is cooled in the second heat-exchanger 52, before being passed through to the device for expansion of the mixture 40.
  • the first flow (from the first output 40a) from the device for expansion of the mixture 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 40b of the device for expansion of the mixture 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 device for expansion of the mixture 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 Figure 6 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-5 will not be repeated with respect to Figure 6.
  • the 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 60a and 60b 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 60b and an input to the rectifying tower 38.
  • the first output 40a of the device for expansion of the mixture 40 is coupled to deliver the first flow from the device for expansion of the mixture 40 to the second gas/liquid separator 60.
  • liquid separation is performed twice: before and after various forms of the mixture are expanded in the device for expansion of the mixture 40. More specifically, the first flow from the device for expansion of the mixture 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 device for expansion of the mixture 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.
  • the gas-phase product, coming from the rectifying tower, can be cooled additionally.
  • 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 Figure 7 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-6 will not be repeated with respect to Figure 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 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 36a 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 Figure 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 second flow from gas/liquid separator 36 before the second 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.
  • At least part of the gas-phase product, coming from the rectifying tower, is supplied to the mixture before its expansion together with part of products obtained by passing the liquid separated from the mixture through the throttling valve.
  • 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 Figure 8 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-7 will not be repeated with respect to Figure 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 device for expansion of the mixture 40. To that end, 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 device for expansion of the mixture 40 where the mixture undergoes the process above described with respect to Figures 1 and 2 to produce the first and second flows.
  • This method allows a deeper purification of the gas flow by removing a greater proportion of components heavier than methane when natural gas is being processed.
  • part of the liquid separated from the mixture is passed through the throttling valve, and the obtained products are used for additional mixture cooling by passing them through the heated channels of the heat exchanger in which the mixture is cooled, and then these products are directed to the mixture before its expansion.
  • 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 Figure 9 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-8 will not be repeated with respect to Figure 9.
  • the 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 36b 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 38a 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 Figures 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.
  • the turbo-expander can be used before or after the mixture expansion.
  • FIG 10 shown is a schematic drawing of a low-temperature gas mixture separation system 1000 according to a ninth embodiment of the invention, referred to as the system 1000 hereinafter for brevity.
  • the system 1000 illustrated in Figure 10 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-9 will not be repeated with respect to Figure 10.
  • the 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. [00112]
  • 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 40b of the device for expansion of the mixture 40 and the first heat-exchanger 32.
  • the system 1000 also includes a second compressor 64 connected in series between the first compressor 42 and the second input 30b of the first mixer 30.
  • the second flow coupled from the second output 40b of the device for expansion of the mixture 40, passes through the turbine 70 and then through the first heat-exchanger 32.
  • a turbo-device for expansion of the mixture may be used to provide additional expansion, either before or after the mixture passes through the device for expansion of the mixture 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 device for expansion of the mixture 40 as described above.
  • the first flow from the device for expansion of the mixture 40 is directed into the second gas/liquid separator 60.
  • the second separator 60 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 Figure 11 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-10 will not be repeated with respect to Figure 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 30a 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 36b 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 device for expansion of the mixture.
  • 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 device for expansion of the mixture. 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. 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 device for expansion of the mixture 40 and undergoes the process described above with respect to Figures 1 and 2.
  • FIG. 12 shown is a schematic drawing of a low-temperature gas mixture separation system 1200 according to a eleventh embodiment of the invention, referred to as the system 1200 hereinafter for brevity.
  • the system 1200 illustrated in Figure 12 is similar to the respective systems illustrated in
  • 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 device for expansion of the mixture 40.
  • the second stream is coupled into the turbine 70 that is placed in parallel with the device for expansion of the mixture 40.
  • the first output 40a of the device for expansion of the mixture 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 40b of the device for expansion of the mixture 40 and the first output 38a 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 device for expansion of the mixture 40. The first flow from the device for expansion of the mixture 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.
  • the gas-phase products, coming from the rectifying tower are cooled and expanded, and part of the products enriched in components heavier than methane are separated, which are directed, either partially or totally, to the rectifying tower.
  • Figure 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 Figure 13 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-12 will not be repeated with respect to Figure 13. Those skilled in the art will appreciate that the 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 device for expansion of the mixture 80 similar in design and function to the device for expansion of the mixture 40 described above with respect to Figure 2.
  • the device for expansion of the mixture 80 has respective first and second outputs 80a and 80b.
  • the first output 80a is connected to deliver a first flow, of heavier components, to the second gas/liquid separator 60
  • the second output 40b 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 60b) 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 device for expansion of the mixture 80) and separated, and the resulting second flow from the second device for expansion of the mixture 80 is directed, either partially or totally, back to the rectifying tower 38.
  • the gas-phase products, coming from the rectifying tower, are additionally compressed in the compressor.
  • FIG 14 as an example, 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 Figure 14 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-13 will not be repeated with respect to Figure 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 38a 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 60a i.e. the gas/vapor output
  • the first output 80a (containing the heavier of the separated components from the expansion and separation process) of the device for expansion of the mixture 80 is coupled to the rectifying tower 38 and the second output 80b is combined with the second output 40b of the device for expansion of the mixture 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 62 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 Figure 13.
  • the gas-phase products, coming from the rectifying tower, are expanded to obtain the product enriched in components heavier than methane; the latter is directed, either partially or totally, to the rectifying tower or returned to the flow of gas-phase products before its expansion.
  • 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 Figure 15 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-14 will not be repeated with respect to Figure 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.
  • the gas-phase products from the rectifying tower 38 are expanded within the second device for expansion of the mixture 80 to separate heavy and light components from one another as described above with respect to Figure 2.
  • the first flow (containing the heavier components) from the first output 80a of the second device for expansion of the mixture 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 80b of the device for expansion of the mixture 80 is combined with the gas/vapor stream output from the second separator 60 and the second output 40b of the device for expansion of the mixture 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.
  • the enriched flow obtained after expansion of the gas-phase product, coming from the rectifying tower is directed to the initial mixture before its expansion.
  • 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 Figure 16 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-15 will not be repeated with respect to Figure 16.
  • the 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 38a of the rectifying tower 38 and the input of the second device for expansion of the mixture 80.
  • the first output 80a of the device for expansion of the mixture 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 device for expansion of the mixture 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 device for expansion of the mixture 80 before the second heat-exchanger 52.
  • the second throttling valve 66 reduces the pressure of the liquid output stream to the first gas/liquid separator 36.
  • 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 Figure 17 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-16 will not be repeated with respect to Figure 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 Figure 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.
  • the gas/vapor output stream of the second gas/liquid separator 60 is coupled into the device for expansion of the mixture 40.
  • the compressor stage of the turbo-device for expansion of the mixture 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 device for expansion of the mixture 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 36.
  • the liquid phase is separated from the mixture, part of which is passed through the throttling valve; the obtained products are used to cool the mixture and directed to the mixture before its expansion.
  • 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 Figure 18 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-17 will not be repeated with respect to Figure 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 36b 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 36b 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 1801 , as shown by example in Figure 18.
  • the incoming mixture 1801 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 1801.
  • the remaining portions of the system operate as described with respect to Figure 3.
  • the mixture before expansion the mixture is separated into at least two flows, one of which is passed through the turbo-expander turbine and directed to the rectifying tower, and the other flow is expanded by passing the swirled mixture flow through the nozzle channel; at the exit of the nozzle channel or its part the mixture flow is separated into, at least, two flows, one of which is enriched in components heavier than methane, while the other flow is depleted in these components; then the enriched flow is directed to the rectifying tower.
  • Figure 19 shown is a schematic drawing of a low-temperature gas mixture separation system 1900 according to a eighteenth embodiment of the invention, referred to as the system 1900 hereinafter for brevity.
  • the system 1900 illustrated in Figure 19 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-18 will not be repeated with respect to Figure 19. Those skilled in the art will appreciate that the 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 device for expansion of the mixture 40.
  • the second stream is coupled into the turbine 70 that is placed in parallel with the device for expansion of the mixture 40.
  • the first output 40a of the device for expansion of the mixture 40 and the output of the turbine 70 are coupled into the rectifying tower 38.
  • the second output 40b of the device for expansion of the mixture 40 and the first output 38a 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 from separator 36 passes through a valve 50 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-device for expansion of the mixture turbine 70 and directed to the rectifying tower 38, and the other flow is expanded through the device for expansion of the mixture 40.
  • the first flow from the device for expansion of the mixture 40 is sent to the rectifying tower 38, while 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.
  • the flow enriched during expansion and part of the mixture passed through the turbo-expander turbine are mixed in the ejector.
  • 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 Figure 20 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-19 will not be repeated with respect to Figure 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, as well as system 1900 may facilitates improved efficiency of the turbo-device for expansion of the mixture turbine 70, thus providing for deeper gas cooling in the turbine 70 and allowing for a greater compression ratio.
  • the mixture flow before expansion is separated into, at least, three flows, one of which is passed through the valve with controlled mass flow rate and directed either to the rectifying tower or mixed with the gas-phase product coming from the tower.
  • 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 Figure 21 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-20 will not be repeated with respect to Figure 20.
  • the 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 36a of the first gas/liquid separator 36 is split between the turbine 70, the device for expansion of the mixture 40 and the third mixer 68.
  • the third mixer 68 also receives the first flow from the device for expansion of the mixture 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 device for expansion of the mixture 40 and the third mixer 68, respectively.
  • the remaining components operate as discussed with reference to Figures 19 and 20. This method makes it possible to stabilize the mass flow rate through the turbo-device for expansion of the mixture turbine 70 in case of variations in the incoming mixture 2101.
  • the liquid phase is separated from the mixture, part of which is passed through the throttling valve and part of the obtained products is used to cool the mixture and directed to the mixture before its expansion.
  • 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 Figure 15 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-21 will not be repeated with respect to Figure 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) 36b of the first gas/liquid separator and the first output 40a of the device for expansion of the mixture 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 36 and the first flow from the device for expansion of the mixture 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. For example, when processing natural gas the gas-phase products produced by the rectifying tower 38 may have very low amounts of components that are heavier than methane.
  • the liquid phase is separated from the mixture, which is passed through the throttling valve, and the obtained products are used to cool the mixture.
  • 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 Figure 23 is similar to the respective systems illustrated in Figures 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 Figure 1 and 3-22 will not be repeated with respect to Figure 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.
  • a portion of the second output 36b of the first gas/liquid separator 36 and the first output 40a of the device for expansion of the mixture 40 are connected and coupled through the second and the third heat- exchangers 52 and 62.
  • the first output 38a 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 device for expansion of the mixture 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)
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  • Chemical Kinetics & Catalysis (AREA)
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  • Physics & Mathematics (AREA)
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  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
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PCT/CA2005/001437 2004-09-24 2005-09-23 Systems and methods for low-temperature gas separation WO2006032139A1 (en)

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MX2007003514A MX2007003514A (es) 2004-09-24 2005-09-23 Sistemas y metodos para separacion de gas a baja temperatura.
BRPI0516049A BRPI0516049B1 (pt) 2004-09-24 2005-09-23 sistemas e métodos para separação de gases à baixa temperatura
GB0705692A GB2432413B (en) 2004-09-24 2005-09-23 Systems and methods for low-temperature gas separation
CN2005800402687A CN101069055B (zh) 2004-09-24 2005-09-23 低温气体分离的系统和方法
AU2005287826A AU2005287826B2 (en) 2004-09-24 2005-09-23 Systems and methods for low-temperature gas separation
EA200700625A EA010564B1 (ru) 2004-09-24 2005-09-23 Способ низкотемпературной сепарации газовой смеси (варианты)
NO20071943A NO20071943L (no) 2004-09-24 2007-04-17 Systemer og fremgangsmater for lavtemperatursgasseparasjon

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RU2004128348/06A RU2272973C1 (ru) 2004-09-24 2004-09-24 Способ низкотемпературной сепарации газа (варианты)

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