US20100287982A1 - Liquefied Natural Gas and Hydrocarbon Gas Processing - Google Patents

Liquefied Natural Gas and Hydrocarbon Gas Processing Download PDF

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Publication number
US20100287982A1
US20100287982A1 US12/466,661 US46666109A US2010287982A1 US 20100287982 A1 US20100287982 A1 US 20100287982A1 US 46666109 A US46666109 A US 46666109A US 2010287982 A1 US2010287982 A1 US 2010287982A1
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United States
Prior art keywords
stream
column
gas
distillation
expanded
Prior art date
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Abandoned
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US12/466,661
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English (en)
Inventor
Tony L. Martinez
John D. Wilkinson
Hank M. Hudson
Kyle T. Cuellar
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Ortloff Engineers Ltd
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Ortloff Engineers Ltd
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Priority to US12/466,661 priority Critical patent/US20100287982A1/en
Assigned to ORTLOFF ENGINEERS, LTD reassignment ORTLOFF ENGINEERS, LTD ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: CUELLAR, KYLE T., MARTINEZ, TONY L., HUDSON, HANK M., WILKINSON, JOHN D.
Priority to BRPI1011152A priority patent/BRPI1011152A2/pt
Priority to MX2011012185A priority patent/MX2011012185A/es
Priority to CA2760963A priority patent/CA2760963A1/en
Priority to MYPI2011005446A priority patent/MY161650A/en
Priority to PCT/US2010/034732 priority patent/WO2010132678A1/en
Priority to GB1121593.6A priority patent/GB2487110A/en
Priority to CN201080021147.9A priority patent/CN102428334B/zh
Publication of US20100287982A1 publication Critical patent/US20100287982A1/en
Priority to CO11160751A priority patent/CO6470814A2/es
Priority to US13/790,873 priority patent/US8794030B2/en
Abandoned legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/061—Natural gas or substitute natural gas
    • F25J3/0615—Liquefied 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
    • F25J3/0204—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
    • F25J3/0214—Liquefied 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
    • F25J3/0204—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
    • F25J2200/30—Processes or apparatus using separation by rectification using a side column in a single pressure 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
    • F25J2200/38—Processes or apparatus using separation by rectification using pre-separation or distributed distillation before a main column system, e.g. in a at least a double 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
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/02—Multiple feed streams, e.g. originating from different sources
    • 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
    • F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/40—Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/50—Arrangement of multiple equipments fulfilling the same process step in parallel

Definitions

  • This invention relates to a process for the separation of ethane and heavier hydrocarbons or propane and heavier hydrocarbons from liquefied natural gas (hereinafter referred to as LNG) combined with the separation of a gas containing hydrocarbons to provide a volatile methane-rich gas stream and a less volatile natural gas liquids (NGL) or liquefied petroleum gas (LPG) stream.
  • LNG liquefied natural gas
  • FIG. 1 is a flow diagram of a base case natural gas processing plant using LNG to provide its refrigeration
  • FIGS. 4 through 8 are flow diagrams illustrating alternative means of application of the present invention to LNG and natural gas streams.
  • FIGS. 1 and 2 are provided to quantify the advantages of the present invention.
  • FIG. 1 is a flow diagram showing the design of a processing plant to recover C 2 + components from natural gas using an LNG stream to provide refrigeration.
  • inlet gas enters the plant at 126° F. [52° C.] and 600 psia [4,137 kPa(a)] as stream 31 .
  • the sulfur compounds are removed by appropriate pretreatment of the feed gas (not illustrated).
  • the feed stream is usually dehydrated to prevent hydrate (ice) formation under cryogenic conditions. Solid desiccant has typically been used for this purpose.
  • Liquid stream 35 is flash expanded through an appropriate expansion device, such as expansion valve 17 , to the operating pressure (approximately 430 psia [2,965 kPa(a)]) of fractionation tower 20 .
  • the expanded stream 35 a leaving expansion valve 17 reaches a temperature of ⁇ 93° F. [ ⁇ 70° C.] and is supplied to fractionation tower 20 at a first mid-column feed point.
  • Overhead distillation stream 43 is withdrawn from the upper section of fractionation tower 20 at ⁇ 143° F. [ ⁇ 97° C.] and is divided into two portions, streams 44 and 47 .
  • the first portion, stream 44 flows to reflux condenser 23 where it is cooled to ⁇ 237° F. [ ⁇ 149° C.] and totally condensed by heat exchange with a portion (stream 72 ) of the cold LNG (stream 71 a ).
  • Condensed stream 44 a enters reflux separator 24 wherein the condensed liquid (stream 46 ) is separated from any uncondensed vapor (stream 45 ).
  • the liquid stream 46 from reflux separator 24 is pumped by reflux pump 25 to a pressure slightly above the operating pressure of demethanizer 20 and stream 46 a is then supplied as cold top column feed (reflux) to demethanizer 20 .
  • This cold liquid reflux absorbs and condenses the C 2 components and heavier hydrocarbon components from the vapors rising in the upper section of demethanizer 20 .
  • the second stage is compressor 21 driven by a supplemental power source which compresses stream 38 c to sales line pressure (stream 38 d ).
  • stream 38 e After cooling to 126° F. [52° C.] in discharge cooler 22 , stream 38 e combines with warm LNG stream 71 b to form the residue gas product (stream 42 ).
  • Residue gas stream 42 flows to the sales gas pipeline at 1262 psia [8,701 kPa(a)], sufficient to meet line requirements.
  • the recoveries reported in Table I are computed relative to the total quantities of ethane, propane, and butanes+ contained in the gas stream being processed in the plant and in the LNG stream. Although the recoveries are quite high relative to the heavier hydrocarbons contained in the gas being processed (99.58%, 100.00%, and 100.00%, respectively, for ethane, propane, and butanes+), none of the heavier hydrocarbons contained in the LNG stream are captured in the FIG. 1 process. In fact, depending on the composition of LNG stream 71 , the residue gas stream 42 produced by the FIG. 1 process may not meet all pipeline specifications.
  • the specific power reported in Table I is the power consumed per unit of liquid product recovered, and is an indicator of the overall process efficiency.
  • FIG. 2 is a flow diagram showing processes to recover C 2 + components from LNG and natural gas in accordance with U.S. Pat. No. 7,216,507 and co-pending application Ser. No. 11/430,412, respectively, with the processed LNG stream used to provide refrigeration for the natural gas plant.
  • the processes of FIG. 2 have been applied to the same LNG stream and inlet gas stream compositions and conditions as described previously for FIG. 1 .
  • the remaining portion of condensed liquid stream 79 b, reflux stream 82 flows to heat exchanger 52 where it is subcooled to ⁇ 237° F. [ ⁇ 149° C.] by heat exchange with a portion of the cold LNG (stream 76 ) as described previously.
  • the subcooled stream 82 a is then expanded to the operating pressure of demethanizer 62 by expansion valve 57 .
  • the expanded stream 82 b at ⁇ 236° F. [ ⁇ 149° C.] is then supplied as cold top column feed (reflux) to demethanizer 62 .
  • This cold liquid reflux absorbs and condenses the C 2 components and heavier hydrocarbon components from the vapors rising in the upper rectification section of demethanizer 62 .
  • the demethanizer in fractionation column 20 is a conventional distillation column containing a plurality of vertically spaced trays, one or more packed beds, or some combination of trays and packing consisting of two sections.
  • the upper absorbing (rectification) section contains the trays and/or packing to provide the necessary contact between the vapors rising upward and cold liquid falling downward to condense and absorb the ethane and heavier components;
  • the lower stripping (demethanizing) section contains the trays and/or packing to provide the necessary contact between the liquids falling downward and the vapors rising upward.
  • the demethanizing section also includes one or more reboilers (such as the side reboiler in heat exchanger 12 described previously, and reboiler 19 using high level utility heat) which heat and vaporize a portion of the liquids flowing down the column to provide the stripping vapors which flow up the column.
  • the column liquid stream 40 exits the bottom of the tower at 89° F. [31° C.], based on a typical specification of a methane to ethane ratio of 0.020:1 on a molar basis in the bottom product, and combines with stream 80 to form the liquid product (stream 41 ).
  • a portion of the distillation vapor (stream 44 ) is withdrawn from the upper region of the stripping section of fractionation column 20 at ⁇ 125° F. [ ⁇ 87° C.] and compressed to 545 psia [3,756 kPa(a)] by compressor 26 .
  • the compressed stream 44 a is then cooled from ⁇ 87° F. [ ⁇ 66° C.] to ⁇ 143° F. [ ⁇ 97° C.] and condensed (stream 44 b ) in heat exchanger 14 by heat exchange with cold overhead distillation stream 38 exiting the top of demethanizer 20 and cold lean LING (stream 83 a ) at ⁇ 116° F. [ ⁇ 82° C.].
  • Condensed liquid stream 44 b is expanded by expansion valve 16 to a pressure slightly above the operating pressure of demethanizer 20 , and the resulting stream 44 c at ⁇ 146° F. [ ⁇ 99° C.] is then supplied as cold liquid reflux to an intermediate region in the absorbing section of demethanizer 20 .
  • This supplemental reflux absorbs and condenses most of the C 3 components and heavier components (as well as some of the C 2 components) from the vapors rising in the lower rectification region of the absorbing section so that only a small amount of recycle (stream 36 ) must be cooled, condensed, subcooled, and flash expanded to produce the top reflux stream 36 c that provides the final rectification in the upper region of the absorbing section of demethanizer 20 .
  • Overhead distillation stream 38 is withdrawn from the upper section of fractionation tower 20 at ⁇ 148° F. [ ⁇ 100° C.]. It passes countercurrently to compressed distillation vapor stream 44 a and recycle stream 36 a in heat exchanger 14 where it is heated to ⁇ 114° F. [ ⁇ 81 ° C.] (stream 38 a ), and countercurrently to inlet gas stream 31 and recycle stream 36 in heat exchanger 12 where it is heated to 20° F. [ ⁇ 7° C.] (stream 38 b ). The distillation stream is then re-compressed in two stages. The first stage is compressor 11 driven by expansion machine 10 . The second stage is compressor 21 driven by a supplemental power source which compresses stream 38 c to sales line pressure (stream 38 d ).
  • stream 38 e After cooling to 126° F. [52° C.] in discharge cooler 22 , stream 38 e is divided into two portions, stream 37 and recycle stream 36 .
  • Stream 37 combines with warm lean LNG stream 83 c to form the residue gas product (stream 42 ).
  • Residue gas stream 42 flows to the sales gas pipeline at 1262 psia [8,701 kPa(a)], sufficient to meet line requirements.
  • the heated stream 71 c enters separator 54 at 11° F. [ ⁇ 12° C.] and 1334 psia [9,198 kPa(a)] where the vapor (stream 77 ) is separated from any remaining liquid (stream 78 ).
  • Vapor stream 77 enters a work expansion machine 55 in which mechanical energy is extracted from the high pressure feed.
  • the machine 55 expands the vapor substantially isentropically to the tower operating pressure (approximately 412 psia [2,839 kPa(a)]), with the work expansion cooling the expanded stream 77 a to a temperature of approximately ⁇ 100° F. [ ⁇ 73° C.].
  • the work recovered is often used to drive a centrifugal compressor (such as item 56 ) that can be used to re-compress a portion (stream 81 ) of the column overhead vapor (stream 79 ), for example.
  • the partially condensed expanded stream 77 a is thereafter supplied as feed to fractionation column 20 at a first mid-column feed point.
  • the separator liquid (stream 78 ), if any, is expanded to the operating pressure of fractionation column 20 by expansion valve 59 before expanded stream 78 a is supplied to fractionation tower 20 at a first lower mid-column feed point.
  • exchanger 12 is representative of either a multitude of individual heat exchangers or a single multi-pass heat exchanger, or any combination thereof. (The decision as to whether to use more than one heat exchanger for the indicated heating services will depend on a number of factors including, but not limited to, inlet gas flow rate, heat exchanger size, stream temperatures, etc.)
  • the vapor (stream 34 ) from separator 13 enters a work expansion machine 10 in which mechanical energy is extracted from this portion of the high pressure feed.
  • the machine 10 expands the vapor substantially isentropically to the operating pressure of fractionation tower 20 , with the work expansion cooling the expanded stream 34 a to a temperature of approximately ⁇ 108° F. [ ⁇ 78° C.].
  • the work recovered is often used to drive a centrifugal compressor (such as item 11 ) that can be used to re-compress the heated distillation stream (stream 38 a ), for example.
  • the expanded partially condensed stream 34 a is supplied to fractionation tower 20 at a second mid-column feed point.
  • Demethanizing section 20 b also includes one or more reboilers (such as the side reboiler in heat exchanger 12 described previously, side reboiler 18 using low level utility heat, and reboiler 19 using high level utility heat) which heat and vaporize a portion of the liquids flowing down the column to provide the stripping vapors which flow up the column.
  • the column liquid stream 41 exits the bottom of the tower at 83° F. [28° C.], based on a typical specification of a methane to ethane ratio of 0.020:1 on a molar basis in the bottom product.
  • a portion of the distillation vapor (stream 44 ) is withdrawn from the upper region of stripping section 20 b of fractionation column 20 at ⁇ 120° F. [ ⁇ 84° C.] and is cooled to ⁇ 143° F. [ ⁇ 97° C.] and condensed (stream 44 a ) in heat exchanger 52 by heat exchange with the cold LNG (stream 71 a ).
  • Condensed liquid stream 44 a is pumped to slightly above the operating pressure of fractionation column 20 by pump 27 , whereupon stream 44 b at ⁇ 143° F. [ ⁇ 97° C.] is then supplied as cold liquid reflux to an intermediate region in absorbing section 20 a of fractionation column 20 .
  • This supplemental reflux absorbs and condenses most of the C 3 components and heavier components (as well as some of the C 2 components) from the vapors rising in the lower rectification region of absorbing section 20 a so that only a small amount of the lean LNG (stream 82 ) must be subcooled to produce the top reflux stream 82 b that provides the final rectification in the upper region of absorbing section 20 a of fractionation column 20 .
  • Overhead distillation stream 79 is withdrawn from the upper section of fractionation tower 20 at ⁇ 145° F. [ ⁇ 98° C.] and is divided into two portions, stream 81 and stream 38 .
  • the first portion (stream 81 ) flows to compressor 56 driven by expansion machine 55 , where it is compressed to 1092 psia [7,529 kPa(a)] (stream 81 a ).
  • the stream is totally condensed as it is cooled to ⁇ 106° F. [ ⁇ 77° C.] in heat exchanger 52 as described previously.
  • the condensed liquid (stream 81 b ) is then divided into two portions, streams 83 and 82 .
  • the first portion (stream 83 ) is the methane-rich lean LNG stream, which is pumped by pump 63 to 1273 psia [8,777 kPa(a)] for subsequent vaporization in heat exchanger 12 , heating stream 83 a to 65° F. [18° C.] as described previously to produce warm lean LNG stream 83 b.
  • the lower top reflux flow plus the greater degree of heating using low level utility heat in heat exchanger 53 , results in less total liquid feeding fractionation column 20 , reducing the duty required in reboiler 19 and minimizing the amount of high level utility heat needed to meet the specification for the bottom liquid product from demethanizer 20 .
  • the rectification of the column vapors provided by absorbing section 20 a allows all of the LNG feed to be vaporized before entering work expansion machine 55 as stream 77 , resulting in significant power recovery.
  • This power can then be used to compress the first portion (stream 81 ) of distillation overhead stream 79 to a pressure sufficiently high so that it can be condensed in heat exchanger 52 and so that the resulting lean LNG (stream 83 ) can then be pumped to the pipeline delivery pressure. (Pumping uses significantly less power than compressing.)
  • this “free” refrigeration of inlet gas stream 31 means less of the cooling duty in heat exchanger 12 must be supplied by distillation vapor stream 38 , so that stream 38 a is cooler and less compression power is needed to raise its pressure to the pipeline delivery condition.
  • a portion of the distillation vapor (stream 44 ) is withdrawn from the upper region of the stripping section of fractionation column 20 at ⁇ 119° F. [ ⁇ 84° C.] and is cooled to ⁇ 145° F. [ ⁇ 98° C.] and condensed (stream 44 a ) in heat exchanger 52 by heat exchange with the cold LNG (stream 71 a ).
  • Condensed liquid stream 44 a is pumped to slightly above the operating pressure of fractionation column 20 by pump 27 , whereupon stream 44 b at ⁇ 144° F. [ ⁇ 98° C.] is then supplied as cold liquid reflux to an intermediate region in the absorbing section of fractionation column 20 .
  • This supplemental reflux absorbs and condenses most of the C 3 components and heavier components (as well as some of the C 2 components) from the vapors rising in the lower rectification region of the absorbing section of fractionation column 20 .
  • the column liquid stream 41 exits the bottom of the tower at 85° F. [29° C.], based on a typical specification of a methane to ethane ratio of 0.020:1 on a molar basis in the bottom product.
  • Overhead distillation stream 79 is withdrawn from the upper section of fractionation tower 20 at ⁇ 144° F. [ ⁇ 98° C.] and is divided into two portions, stream 81 and stream 38 .
  • the first portion (stream 81 ) flows to compressor 56 driven by expansion machine 55 , where it is compressed to 929 psia [6,405 kPa(a)] (stream 81 a ). At this pressure, the stream is totally condensed as it is cooled to ⁇ 108° F.
  • the condensed liquid (stream 81 b ) is then divided into two portions, streams 83 and 82 .
  • the first portion (stream 83 ) is the methane-rich lean LNG stream, which is pumped by pump 63 to 1273 psia [8,777 kPa(a)] for subsequent vaporization in heat exchanger 12 , heating stream 83 a to 65° F. [18° C.] as described previously to produce warm lean LNG stream 83 b.
  • FIG. 5 Another alternative method of processing LNG and natural gas is shown in the embodiment of the present invention as illustrated in FIG. 5 .
  • the LNG stream and inlet gas stream compositions and conditions considered in the process presented in FIG. 5 are the same as those in FIGS. 1 through 4 . Accordingly, the FIG. 5 process can be compared with the FIGS. 1 and 2 processes to illustrate the advantages of the present invention, and can likewise be compared to the embodiments displayed in FIGS. 3 and 4 .
  • the heated stream 71 c enters separator 54 at 1° F. [ ⁇ 17° C.] and 1334 psia [9,198 kPa(a)] where the vapor (stream 77 ) is separated from any remaining liquid (stream 78 ).
  • Vapor stream 77 enters a work expansion machine 55 in which mechanical energy is extracted from the high pressure feed.
  • the machine 55 expands the vapor substantially isentropically to the tower operating pressure (approximately 395 psia [2,721 kPa(a)]), with the work expansion cooling the expanded stream 77 a to a temperature of approximately ⁇ 107° F. [ ⁇ 77° C.].
  • the partially condensed expanded stream 77 a is thereafter supplied as feed to fractionation column 20 at a first mid-column feed point.
  • the separator liquid (stream 78 ), if any, is expanded to the operating pressure of fractionation column 20 by expansion valve 59 before expanded stream 78 a is supplied to fractionation tower 20 at a first lower mid-column feed point.
  • the cooled stream 31 b enters separator 13 at ⁇ 81° F. [ ⁇ 63° C.] and 403 psia [2,777 kPa(a)] where the vapor (stream 34 ) is separated from the condensed liquid (stream 35 ).
  • Vapor stream 34 is cooled to ⁇ 117° F. [ ⁇ 83° C.] in heat exchanger 52 by heat exchange with cold LNG stream 71 a and compressed distillation stream 38 a, and the partially condensed stream 34 a is then supplied to fractionation tower 20 at a second mid-column feed point.
  • Liquid stream 35 is directed through valve 17 and is supplied to fractionation tower 20 at a second lower mid-column feed point.
  • the column liquid stream 41 exits the bottom of the tower at 79° F. [26° C.], based on a typical specification of a methane to ethane ratio of 0.020:1 on a molar basis in the bottom product.
  • Overhead distillation stream 79 is withdrawn from the upper section of fractionation tower 20 at ⁇ 147° F. [ ⁇ 99° C.] and is divided into two portions, stream 81 and stream 38 .
  • the first portion (stream 81 ) flows to compressor 56 driven by expansion machine 55 , where it is compressed to 1124 psia [7,750 kPa(a)] (stream 81 a ). At this pressure, the stream is totally condensed as it is cooled to ⁇ 103° F.
  • the condensed liquid (stream 81 b ) is then divided into two portions, streams 83 and 82 .
  • the first portion (stream 83 ) is the methane-rich lean LNG stream, which is pumped by pump 63 to 1273 psia [8,777 kPa(a)] for subsequent vaporization in heat exchanger 12 , heating stream 83 a to 65° F. [18° C.] as described previously to produce warm lean LNG stream 83 b.
  • stream 81 b flows to heat exchanger 52 where it is subcooled to ⁇ 236° F. [ ⁇ 149° C.] by heat exchange with the cold LNG (stream 71 a ) as described previously.
  • the subcooled stream 82 a is expanded to the operating pressure of fractionation column 20 by expansion valve 57 .
  • the expanded stream 82 b at ⁇ 233° F. [ ⁇ 147° C.] is then supplied as cold top column feed (reflux) to demethanizer 20 .
  • This cold liquid reflux absorbs and condenses the C 2 components and heavier hydrocarbon components from the vapors rising in the upper rectification region of the absorbing section of demethanizer 20 .
  • the distillation stream is then further compressed to sales gas line pressure (stream 38 d ) in compressor 21 driven by a supplemental power source, and stream 38 d / 38 e then combines with warm lean LNG stream 83 b to form the residue gas product (stream 42 ).
  • Residue gas stream 42 at 107° F. [42° C.] flows to the sales gas pipeline at 1262 psia [8,701 kPa(a)], sufficient to meet line requirements.
  • Pump 67 is used to route the liquids (stream 46 ) from the bottom of absorber column 66 to the top of stripper column 20 so that the two towers effectively function as one distillation system.
  • the decision whether to construct the fractionation tower as a single vessel (such as demethanizer 20 in FIGS. 3 through 5 ) or multiple vessels will depend on a number of factors such as plant size, the distance to fabrication facilities, etc.
  • total condensation of streams 44 a and 81 b is illustrated in FIGS. 3 through 8 .
  • Some circumstances may favor subcooling these streams, while other circumstances may favor only partial condensation. Should partial condensation of either or both of these streams be achieved, processing of the uncondensed vapor may be necessary, using a compressor or other means to elevate the pressure of the vapor so that it can join the pumped condensed liquid. Alternatively, the uncondensed vapor could be routed to the plant fuel system or other such use.
  • the heated LNG stream leaving heat exchanger 53 may not contain any liquid (because it is above its dewpoint, or because it is above its cricondenbar). In such cases, separator 54 and expansion valve 59 may be eliminated as shown by the dashed lines.
  • the use and distribution of the methane-rich lean LNG and distillation vapor streams for process heat exchange, and the particular arrangement of heat exchangers for heating the LNG streams and cooling the feed gas stream, must be evaluated for each particular application, as well as the choice of process streams for specific heat exchange services.
  • lean LNG stream 83 a is used directly to provide cooling in heat exchanger 12 .
  • some circumstances may favor using the lean LNG to cool an intermediate heat transfer fluid, such as propane or other suitable fluid, whereupon the cooled heat transfer fluid is then used to provide cooling in heat exchanger 12 .
  • This alternative means of indirectly using the refrigeration available in lean LNG stream 83 a accomplishes the same process objectives as the direct use of stream 83 a for cooling in the FIGS. 3 through 8 embodiments of the present invention.
  • the choice of how best to use the lean LNG stream for refrigeration will depend mainly on the composition of the inlet gas, but other factors may affect the choice as well.

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MYPI2011005446A MY161650A (en) 2009-05-15 2010-05-13 Liquefied natural gas and hydrocarbon gas processing
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BRPI1011152A BRPI1011152A2 (pt) 2009-05-15 2010-05-13 processamento de gás de hidrocarboneto e gás natural liquefeito
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CO11160751A CO6470814A2 (es) 2009-05-15 2011-11-23 Procesamiento de gas natural licuado y gas hidrocarburo
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US20130283853A1 (en) 2013-10-31
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