Classifications

• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
  • F25J3/0209—Natural gas or substitute natural gas
  • 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
  • F25J3/0228—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
  • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
  • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
  • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
  • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2200/00—Processes or apparatus using separation by rectification
  • F25J2200/02—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
  • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2200/00—Processes or apparatus using separation by rectification
  • F25J2200/72—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
  • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • 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
  • F25J2215/00—Processes characterised by the type or other details of the product stream
  • F25J2215/62—Ethane or ethylene
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
  • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
  • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
  • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2270/00—Refrigeration techniques used
  • F25J2270/02—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
  • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
  • F25J2290/10—Mathematical formulae, modeling, plot or curves; Design methods

Definitions

• contemplated LNG processing plants comprise a pump that pumps at least one of the first and second portions to a feed pressure, and further include a demethanizer that receives at least part of the second portion at a pressure lower than the feed pressure.
• the demethanizer produces an overhead product, wherein a heat exchanger cools at least part of the demethanizer overhead vapor to thereby produce a reflux stream for the demethanizer, and/or wherein a heat exchanger condenses at least part of the overhead vapor from the demethanizer reflux drum to thereby produce the lean LNG.
• contemplated LNG processing plants are configured to combine the first portion and the lean LNG to thereby form the processed LNG, and the processed LNG is then pumped and vaporized at pipeline pressure in a manner well known in the art.
• contemplated plants may also include a control circuit that is configured to control a mass flow ratio between the first and second portion. Using such control circuits, it should be appreciated that the heating value of the combined processed and unprocessed LNG can be maintained at a predetermined level while the LNG entering the plant may have variable chemical compositions and/or heating values.
• the plant may further include a turbo-generator that is driven by expansion of a heated and pressurized portion of the first portion of LNG to thereby produce energy.
• Figure 2 is a schematic view of a second exemplary plant according to the inventive subject matter with removal or recovery of over 70% of ethane and 99% of propane in the inlet LNG.
• Figure 3 is a schematic view of a third exemplary plant according to the inventive subject matter with removal or recovery of 99% of propane in the inlet LNG using an integral reflux condensing exchanger.
• Figure 4 is a schematic view of a fourth exemplary plant according to the inventive subject matter for a plant that recovers C 2 and C 3 while producing energy.
• Figure 7 is a schematic view of a seventh exemplary plant according to the inventive subject matter for propane or ethane delivery using a batching NGL pipeline.
• Figure 8 is a graph depicting heating values of LNG from various LNG export plants in the Atlantic, Pacific and Middle East market.
• Such configurations advantageously allow removal or recovery of at least 99% propane and over 70% ethane from the LNG.
• the demethanizer bottoms can be further processed in a deethanizer column to , produce a C2 overhead liquid, and a C3+ bottoms product wherein ethane rejection or varying ethane recovery can be efficiently achieved by diverting at least a portion of the liquid ethane product from the deethanizer overhead to blend with the lean LNG.
• LNG is pumped and split into two portions (streams 2 and 3) as needed for heating value control.
• Stream 3 is letdown in pressure in valve 53 to form stream 4 at about 450 to 500 psig that is heated and partially vaporized in exchanger 54 by heat exchange with the demethanizer overhead stream 8 and reflux separator vapor stream 10.
• the exchanger outlet stream 5 is at about -120°F to -14O 0 F and is further heated in preheater 55 using a heat transfer medium (e.g., glycol (stream 91)) forming stream 6 at about -120°F to -115°F.
• the two-phase stream 6 is then fed to the upper section of demethanizer 56.
• the demethanizer produces a lean natural overhead vapor 8, which is reduced in (or even depleted of) propane and heavier components and at least partially depleted of ethane.
• Demethanizer 56 preferably operates at 450 psig to 500 psig. It should be especially noted that side reboiler 57 can be used to assist the stripping of the light components in stream 17 withdrawn from the lower section of the demethanizer, with heat supplied from glycol stream 92.
• the demethanizer bottom composition is controlled by temperature of stream 7, at about 100 0 F (ethane recovery) to 200 0 F (propane recovery only), using bottom reboiler 58.
• the set point of the demethanizer bottom temperature will control the levels of recovery and provide heating value control of the inlet LNG.
• Bottom product 7 can then be let down in pressure using valve 63 and sent out as LPG stream 20.
• the so generated two-phase stream 9 is then separated in separator 59 into a liquid stream 11 and a lean vapor stream 10.
• Liquid stream 11, containing residual propane and/or ethane components, is pumped by reflux pump 60 and returned to the top of the demethanizer as a cold reflux stream 12.
• the separator vapor stream 10 is returned to exchanger 54 and further cooled and condensed forming stream 13.
• overhead exchanger 54 provides two functions, providing reflux to the demethanizer that is essential to achieve a high propane and ethane recovery, and to condense the separator vapor to a liquid that allows the liquid to be pumped, thus substantially reducing capital and operational cost.
• the lean liquid stream 13, typically at a temperature of about -130° to -140°F is pumped by pump 61 to about 1000 psig pressure as necessary for pipeline transportation or combination with rich LNG stream 2.
• the pressurized lean LNG stream 14 is mixed with stream 2 of the rich LNG and further heated in vaporizer 62 to about 50°F, or other temperature needed to meet pipeline requirements.
• suitable heat sources for the LNG vaporizer include all known heat sources (direct heat sources such as fired heaters, seawater exchangers, etc., or indirect heat sources such as glycol heat transfer systems).
• Valves 52 and 53 are preferably regulated by a control system (not shown) that adjusts the mass flow between streams 2 and 3 to a predetermined ratio (most typically to achieve a desired chemical composition and/or heating value).
• contemplated heat integration and process configurations can also be used for ethane recovery as depicted in the exemplary plant configuration of Figure 2.
• ethane recovery can be varied from 5% up to 80% as needed for heating value control of the rich LNG stream 1.
• numerals of the components of Figure 2 it should be noted that same components of Figures 1 and 2 have same numerals in Figure 2.
• the front end of the configuration according to Figure 2 is similar to that shown in Figure 1.
• a second column 64 (the deethanizer) is added such that the deethanizer receives liquid stream 7 from the demethanizer 56.
• Stream 7 is letdown using valve 63 to a pressure of about 200 psig to 350 psig to form stream 19 that is fed to the mid section of deethanizer 64.
• the operating pressure of the deethanizer can be varied as needed to meet the pressure requirements of the ethane product.
• the deethanizer overhead stream 21 is advantageously at least partially condensed in exchanger 65 using the refrigeration content of lean LNG stream 14.
• the two-phase stream 22 at about O 0 F to 30°F is separated in separator 66 into a liquid stream 23 and an ethane vapor product stream 25.
• a portion of the liquid stream is pumped by reflux pump 67 and returned to the deethanizer overhead as reflux stream 24.
• reflux pump 67 is pumped by reflux pump 67 and returned to the deethanizer overhead as reflux stream 24.
• a portion of the liquid can be produced as stream 26.
• the ethane vapor can be used as a fuel source in the submerged combustion LNG vaporizer, used to fuel a power plant, and/or for petrochemical production.
• the deethanizer produces a bottom product stream 20 with heat supplied by reboiler 68 (e.g., using a glycol heat transfer system as a heat source).
• Lean cooled LNG stream 15 can then be combined with the rich LNG and vaporized in heater 62 to form pipeline gas 16 having desired chemical composition and/or heating value.
• the overhead reflux exchanger in the demethanizer can be integrated in the column as shown in the exemplary plant configuration of Figure 3.
• pumped rich LNG is used in an overhead reflux condenser 69 integral to the column, producing an internal reflux stream 10 that is free flowing to the lower section of the column.
• the heated LNG stream 6 from exchanger 69 is sent to the upper section of the demethanizer, below the reflux exchanger 69.
• contemplated configurations (by virtue of modifying the split ratio of the inlet LNG stream and temperature in the heating value control section) allow processing of LNG with varying compositions and heat contents while producing an "on spec" natural gas and/or LNG transportation fuel for the North American market or other emission sensitive markets.
• contemplated configurations will produce high-purity ethane as commercial product or as energy source for the combined cycle power plant.
• contemplated plants may comprise a pump and a heat source that heats a first portion of a liquefied natural gas, and an expander in which the pumped and heated liquefied natural gas is expanded to produce work. It is still further preferred that at least a portion of the expanded gas is fed into a demethanizer as a stripping gas to produce a lean gas (at least partially depleted from ethane) and a demethanized bottom product, wherein the lean gas maybe re-condensed using at least part of the refrigeration content of the LNG.
• the demethanizer bottom product may then be fed to a deethanizer that produces an ethane product and a liquefied petroleum gas product.
• At least a portion of the reflux condenser duty of the demethanizer and deethanizer is provided by the refrigeration content of a portion of the liquefied natural gas before the heat source heats the liquid portion of the liquefied natural gas, and/or that a second portion of the liquefied natural gas (vapor portion) is separated in a demethanizer into a lean gas and a demethanized bottom product.
• Figure 4 exemplarily depicts a configuration in which power is generated and in which C 2 and C 3 components are recovered
• Figure 5 exemplarily depicts a configuration in which power is generated and in which C 3 components are recovered.
• the LNG is separated in a separator 151.
• the separator vapor stream 101 is fed to the upper section of the demethanizer 56, and the separator liquid stream 102 is pumped by LNG booster pump 152 to about 2500 psig to 3500 psig forming stream 103.
• the pressurized liquid is heated by an external heat source in exchanger 153 using a heat medium 99 forming stream 104 at about 400 0 F to 500°F.
• Various heat sources can be applied, including waste heat sources from flue gas, process waste heat, and ambient heat and/ or fuel fired combustion heater, and the choice depends on availability and economics.
• Stream 104 is then expanded in an expander 154 to stream 105 at a pressure of about 400 psig to 500 psig, generating about 15,000 HP that can be used to supply the power requirement in the regasification process including pump 152 with the excess power being exported for sales.
• Demethanizer overhead 8 is re-condensed in exchanger 54, separated in separator 59 with the liquid pumped by pump 60 to form stream 12, and with the lean LNG 14 (via 10 and 13) being further heated in exchanger 65 and 62.
• higher expander inlet pressure may be used to increase power output and efficiency.
• higher expander pressure is only desirable where electric power can be sold at a premium.
• an LNG plant can also be operated in an ethane recovery or ethane rejection (propane recovery) mode as depicted in the exemplary plant configuration of Figure 6.
• ethane recovery can be varied from about 2% to about 80% as needed to meet the ethane market demand.
• the term "about” where used herein in conjunction with a numeral refers to a +/- 10% range of that numeral.
• the configuration of such process is similar to that of Figure 2 with some variations.
• contemplated configurations provide a highly efficient LNG power generation cycle that can be coupled with a heating control unit utilizing fractionation, and re-condensation.
• configurations contemplated herein allow LNG regasification plants to be less dependent on an external power supply, thus making such configurations even more economical and flexible while at the same time providing the capability of processing of LNG with varying compositions and heat contents to meet pipeline specifications.
• heating of the first portion is provided by a heat transfer fluid (e.g., a glycol water mixture) that transfers heat from heat sources, such as fuel fired heater, ambient air, water circulating system, the gas turbine combustion air, the steam turbine discharge, the heat recovery unit, and/or the flue gas stream.
• a heat transfer fluid e.g., a glycol water mixture
• contemplated plants will receive a liquid natural gas feed that is split in a first portion and a second portion, wherein the first portion enters the heating value control section, and wherein the second portion is fed to the vaporizer (most preferably after combination with the lean LNG).
• LPG is the C 3 + bottom fraction of the demethanizer stream 20, and the pipeline gas is depicted as stream 16 .

Landscapes

• Engineering & Computer Science (AREA)
• Physics & Mathematics (AREA)
• Mechanical Engineering (AREA)
• Thermal Sciences (AREA)
• General Engineering & Computer Science (AREA)
• Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• General Chemical & Material Sciences (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• Separation By Low-Temperature Treatments (AREA)
• Filling Or Discharging Of Gas Storage Vessels (AREA)

Applications Claiming Priority (3)

Publications (2)

Family

ID=35783200

Family Applications (1)

Country Status (8)

Families Citing this family (36)

Family Cites Families (14)

• 2005
  • 2005-06-27 WO PCT/US2005/022880 patent/WO2006004723A1/en not_active Ceased
  • 2005-06-27 EA EA200700221A patent/EA010743B1/ru not_active IP Right Cessation
  • 2005-06-27 CA CA002574601A patent/CA2574601C/en not_active Expired - Fee Related
  • 2005-06-27 US US11/658,110 patent/US20080264100A1/en not_active Abandoned
  • 2005-06-27 AU AU2005259965A patent/AU2005259965B2/en not_active Ceased
  • 2005-06-27 MX MX2007000929A patent/MX2007000929A/es unknown
  • 2005-06-27 EP EP05763868.6A patent/EP1782010A4/de not_active Withdrawn
• 2007
  • 2007-01-29 NO NO20070553A patent/NO334716B1/no not_active IP Right Cessation

Also Published As

Similar Documents

Legal Events