EP2553367A1 - Traitement des gaz hydrocarbonés - Google Patents

Traitement des gaz hydrocarbonés

Info

Publication number
EP2553367A1
EP2553367A1 EP11766369A EP11766369A EP2553367A1 EP 2553367 A1 EP2553367 A1 EP 2553367A1 EP 11766369 A EP11766369 A EP 11766369A EP 11766369 A EP11766369 A EP 11766369A EP 2553367 A1 EP2553367 A1 EP 2553367A1
Authority
EP
European Patent Office
Prior art keywords
stream
receive
distillation
mass transfer
heat exchange
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP11766369A
Other languages
German (de)
English (en)
Inventor
Andrew F. Johnke
W. Larry Lewis
L. Don Tyler
John D. Wilkinson
Joe T. Lynch
Hank M. Hudson
Kyle T. Cuellar
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Ortloff Engineers Ltd
SME Products LP
Original Assignee
Ortloff Engineers Ltd
SME Products LP
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
Priority claimed from PCT/US2010/029331 external-priority patent/WO2010144172A1/fr
Priority claimed from US12/750,862 external-priority patent/US8881549B2/en
Priority claimed from US12/772,472 external-priority patent/US9933207B2/en
Priority claimed from US12/781,259 external-priority patent/US9939195B2/en
Priority claimed from US13/048,315 external-priority patent/US9052136B2/en
Application filed by Ortloff Engineers Ltd, SME Products LP filed Critical Ortloff Engineers Ltd
Priority claimed from US13/051,682 external-priority patent/US9074814B2/en
Publication of EP2553367A1 publication Critical patent/EP2553367A1/fr
Withdrawn legal-status Critical Current

Links

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
    • 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
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • C10G5/04—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas with liquid absorbents
    • 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
    • C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
    • C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
    • 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
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
    • C10G70/041—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by distillation
    • 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
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
    • C10G70/046—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by adsorption, i.e. with the use of solids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1025—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
    • 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
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/80—Processes or apparatus using separation by rectification using integrated mass and heat exchange, i.e. non-adiabatic rectification in a reflux exchanger or dephlegmator
    • 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
    • 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
    • F25J2210/06—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
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
    • 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.

Definitions

  • Propylene, propane, and/or heavier hydrocarbons can be recovered from a variety of gases, such as natural gas, refinery gas, and synthetic gas streams obtained from other hydrocarbon materials such as coal, crude oil, naphtha, oil shale, tar sands, and lignite.
  • Natural gas usually has a major proportion of methane and ethane, i.e., methane and ethane together comprise at least 50 mole percent of the gas.
  • the gas also contains relatively lesser amounts of heavier hydrocarbons such as propane, butanes, pentanes, and the like, as well as hydrogen, nitrogen, carbon dioxide, and other gases.
  • the present invention is generally concerned with the recovery of propylene, propane, and heavier hydrocarbons from such gas streams.
  • a typical analysis of a gas stream to be processed in accordance with this invention would be, in approximate mole percent, 88.4% methane, 6.2% ethane and other C 2 components, 2.6% propane and other C 3 components, 0.3% iso-butane, 0.6% normal butane, and 0.8% pentanes plus, with the balance made up of nitrogen and carbon dioxide. Sulfur containing gases are also sometimes present.
  • a feed gas stream under pressure is cooled by heat exchange with other streams of the process and/or external sources of refrigeration such as a propane compression-refrigeration system.
  • liquids may be condensed and collected in one or more separators as high-pressure liquids containing some of the desired C 3 + components.
  • the high-pressure liquids may be expanded to a lower pressure and fractionated. The vaporization occurring during expansion of the liquids results in further cooling of the stream. Under some conditions, pre-cooling the high pressure liquids prior to the expansion may be desirable in order to further lower the temperature resulting from the expansion.
  • the expanded stream comprising a mixture of liquid and vapor, is fractionated in a distillation (deethanizer) column.
  • the expansion cooled stream(s) is (are) distilled to separate residual methane, C 2 components, nitrogen, and other volatile gases as overhead vapor from the desired C 3 components and heavier hydrocarbon components as bottom liquid product.
  • the vapor remaining from the partial condensation can be passed through a work expansion machine or engine, or an expansion valve, to a lower pressure at which additional liquids are condensed as a result of further cooling of the stream.
  • the expanded stream then enters an absorbing section in the column and is contacted with cold liquids to absorb the C 3 components and heavier components from the vapor portion of the expanded stream.
  • the liquids from the absorbing section are then directed to the deethanizing section of the column.
  • a distillation vapor stream is withdrawn from the upper region of the deethanizing section and is cooled by heat exchange relation with the overhead vapor stream from the absorbing section, condensing at least a portion of the distillation vapor stream.
  • the condensed liquid is separated from the cooled distillation vapor stream to produce a cold liquid reflux stream that is directed to the upper region of the absorbing section, where the cold liquids can contact the vapor portion of the expanded stream as described earlier.
  • the vapor portion (if any) of the cooled distillation vapor stream and the overhead vapor from the absorbing section combine to form the residual methane and C 2 component product gas.
  • the present invention employs a novel means of performing the various steps described above more efficiently and using fewer pieces of equipment. This is accomplished by combining what heretofore have been individual equipment items into a common housing, thereby reducing the plot space required for the processing plant and reducing the capital cost of the facility. Surprisingly, applicants have found that the more compact arrangement also significantly reduces the power consumption required to achieve a given recovery level, thereby increasing the process efficiency and reducing the operating cost of the facility. In addition, the more compact arrangement also eliminates much of the piping used to interconnect the individual equipment items in traditional plant designs, further reducing capital cost and also eliminating the associated flanged piping connections.
  • piping flanges are a potential leak source for hydrocarbons (which are volatile organic compounds, VOCs, that contribute to greenhouse gases and may also be precursors to atmospheric ozone formation), eliminating these flanges reduces the potential for atmospheric emissions that can damage the environment.
  • FIG. 1 is a flow diagram of a prior art natural gas processing plant in accordance with United States Patent No. 5,799,507;
  • FIG. 2 is a flow diagram of a natural gas processing plant in accordance with the present invention.
  • FIGS. 3 through 21 are flow diagrams illustrating alternative means of application of the present invention to a natural gas stream.
  • FIG. 1 is a process flow diagram showing the design of a processing plant to recover C 3 + components from natural gas using prior art according to U.S. Pat. No. 5,799,507.
  • inlet gas enters the plant at 110°F [43°C] and 885 psia [6,100 kPa(a)] as stream 31. If the inlet gas contains a concentration of sulfur compounds which would prevent the product streams from meeting specifications, the sulfur compounds are removed by appropriate
  • the feed stream is usually dehydrated to prevent hydrate (ice) formation under cryogenic conditions.
  • Solid desiccant has typically been used for this purpose.
  • the feed stream 31 is cooled in heat exchanger 10 by heat exchange with cool residue gas (stream 44), flash expanded separator liquids (stream 35a), and distillation liquids at -105°F [-76°C] (stream 43).
  • the cooled stream 31a enters separator 11 at -34°F [-36°C] and 875 psia [6,031 kPa(a)] where the vapor (stream 34) is separated from the condensed liquid (stream 35).
  • the separator liquid (stream 35) is expanded to slightly above the operating pressure (approximately 375 psia
  • the vapor (stream 34) from separator 11 enters a work expansion machine 13 in which mechanical energy is extracted from this portion of the high pressure feed.
  • the machine 13 expands the vapor substantially isentropically to the operating pressure of fractionation tower 15, with the work expansion cooling the expanded stream 34a to a temperature of approximately -100°F [-74°C].
  • the typical commercially available expanders are capable of recovering on the order of 80-85% of the work theoretically available in an ideal isentropic expansion.
  • the work recovered is often used to drive a centrifugal compressor (such as item 14) that can be used to re-compress the heated residue gas (stream 44a), for example.
  • the partially condensed expanded stream 34a is thereafter supplied as feed to fractionation tower 15 at an upper mid-column feed point.
  • the deethanizer in tower 15 is a conventional distillation column containing a plurality of vertically spaced trays, one or more packed beds, or some combination of trays and packing.
  • the deethanizer tower consists of two sections: an upper absorbing (rectification) section 15a that contains the trays and/or packing to provide the necessary contact between the vapor portion of the expanded stream 34a rising upward and cold liquid falling downward to condense and absorb the C 3 components and heavier components; and a lower stripping section 15b that contains the trays and/or packing to provide the necessary contact between the liquids falling downward and the vapors rising upward.
  • the deethanizing section 15b also includes at least one reboiler (such as reboiler 16) which heats and vaporizes a portion of the liquids flowing down the column to provide the stripping vapors which flow up the column to strip the liquid product, stream 37, of methane, C 2 components, and lighter components.
  • Stream 34a enters deethanizer 15 at a mid-column feed position located in the lower region of absorbing section 15a of deethanizer 15. The liquid portion of expanded stream 34a commingles with liquids falling downward from absorbing section 15a and the combined liquid continues downward into stripping section 15b of deethanizer 15.
  • a portion of the distillation vapor (stream 38) is withdrawn from the upper region of stripping section 15b. This stream is then cooled and partially condensed (stream 38a) in exchanger 17 by heat exchange with cold deethanizer overhead stream 36 which exits the top of deethanizer 15 at -109°F [-79°C].
  • the cold deethanizer overhead stream is warmed to approximately -33°F [-66°C] (stream 36a) as it cools stream 38 from -30°F [-35°C] to about -103°F [-75°C] (stream 38a).
  • the operating pressure in reflux separator 18 is maintained slightly below the operating pressure of deethanizer 15. This pressure difference provides the driving force that allows distillation vapor stream 38 to flow through heat exchanger 17 and thence into the reflux separator 18 wherein the condensed liquid (stream 40) is separated from the uncondensed vapor (stream 39).
  • the uncondensed vapor stream 39 combines with the warmed deethanizer overhead stream 36a from exchanger 17 to form cool residue gas stream 44 at -37°F [-38°C].
  • the liquid stream 40 from reflux separator 18 is pumped by pump 19 to a pressure slightly above the operating pressure of deethanizer 15.
  • the resulting stream 40a is then divided into two portions.
  • the first portion (stream 41) is supplied as cold top column feed (reflux) to the upper region of absorbing section 15a of deethanizer 15.
  • This cold liquid causes an absorption cooling effect to occur inside the absorbing (rectification) section 15a of deethanizer 15, wherein the saturation of the vapors rising upward through the tower by vaporization of liquid methane and ethane contained in stream 41 provides refrigeration to the section.
  • both the vapor leaving the upper region (overhead stream 36) and the liquids leaving the lower region (distillation liquid stream 43) of absorbing section 15a are colder than the either of the feed streams (streams 41 and stream 34a) to absorbing section 15a.
  • This absorption cooling effect allows the tower overhead (stream 36) to provide the cooling needed in heat exchanger 17 to partially condense the distillation vapor stream (stream 38) without operating stripping section 15b at a pressure significantly higher than that of absorbing section 15a.
  • This absorption cooling effect also facilitates reflux stream 41 condensing and absorbing the C 3 components and heavier components in the distillation vapor flowing upward through absorbing section 15a.
  • the second portion (stream 42) of pumped stream 40a is supplied to the upper region of stripping section 15b of deethanizer 15 where the cold liquid acts as reflux to absorb and condense the C 3 components and heavier components flowing upward from below so that distillation vapor stream 38 contains minimal quantities of these components.
  • a distillation liquid stream 43 from deethanizer 15 is withdrawn from the lower region of absorbing section 15a and is routed to heat exchanger 10 where it is heated as it provides cooling of the incoming feed gas as described earlier.
  • thermosiphon circulation Typically the flow of this liquid from the deethanizer is via thermosiphon circulation, but a pump could be used.
  • the liquid stream is heated to -4°F [-20°C], partially vaporizing stream 43a before it is returned as a mid-column feed to deethanizer 15, in the middle region of stripping section 15b.
  • the feed streams are stripped of their methane and C 2 components.
  • the resulting liquid product stream 37 exits the bottom of the tower at 201 °F [94°C] based on a typical specification of an ethane to propane ratio of 0.048:1 on a molar basis in the bottom product.
  • the cool residue gas (stream 44) passes countercurrently to the incoming feed gas in heat exchanger 10 where it is heated to 98°F [37°C] (stream 44a).
  • the residue gas is then re-compressed in two stages.
  • the first stage is compressor 14 driven by expansion machine 13.
  • the second stage is compressor 20 driven by a supplemental power source which compresses the residue gas (stream 44c) to sales line pressure.
  • residue gas stream 44d flows to the sales gas pipeline at 915 psia [6,307 kPa(a)], sufficient to meet line requirements
  • FIG. 2 illustrates a flow diagram of a process in accordance with the present invention.
  • the feed gas composition and conditions considered in the process presented in FIG. 2 are the same as those in FIG. 1. Accordingly, the FIG. 2 process can be compared with that of the FIG. 1 process to illustrate the advantages of the present invention.
  • inlet gas enters the plant as stream 31 and enters a heat exchange means in feed cooling section 115a inside processing assembly 115.
  • This heat exchange means may be comprised of a fin and tube type heat exchanger, a plate type heat exchanger, a brazed aluminum type heat exchanger, or other type of heat transfer device, including multi-pass and/or multi-service heat exchangers.
  • the heat exchange means is configured to provide heat exchange between stream 31 flowing through one pass of the heat exchange means and flash expanded separator liquids (stream 35a) and a residue gas stream from condensing section 115b inside processing assembly 115.
  • Stream 31 is cooled while heating the flash expanded separator liquids and the residue gas stream.
  • a first portion (stream 32) of stream 31 is withdrawn from the heat exchange means after stream 31 has been partially cooled to 25°F [-4°C], while the remaining second portion (stream 33) is further cooled so that it leaves the heat exchange means at -20°F [-29°C].
  • Separator section 115e has an internal head or other means to divide it from deethanizing section 115d, so that the two sections inside processing assembly 115 can operate at different pressures.
  • the first portion (stream 32) of stream 31 enters the lower region of separator section 115e at 875 psia [6,031 kPa(a)] where any condensed liquid is separated from the vapor before the vapor is directed into a heat and mass transfer means inside separator section 115e.
  • This heat and mass transfer means may also be comprised of a fin and tube type heat exchanger, a plate type heat exchanger, a brazed aluminum type heat exchanger, or other type of heat transfer device, including multi-pass and/or multi-service heat exchangers.
  • the heat and mass transfer means is configured to provide heat exchange between the vapor portion of stream 32 flowing upward through one pass of the heat and mass transfer means and distillation liquid stream 43 from absorbing section 115c inside processing assembly 115 flowing downward, so that the vapor is cooled while heating the distillation liquid stream. As the vapor stream is cooled, a portion of it may be condensed and fall downward while the remaining vapor continues flowing upward through the heat and mass transfer means.
  • the heat and mass transfer means provides continuous contact between the condensed liquid and the vapor so that it also functions to provide mass transfer between the vapor and liquid phases to provide partial rectification of the vapor. [0030]
  • the second portion (stream 33) of stream 31 enters separator section
  • the vapor (stream 34) from separator section 115e enters a work expansion machine 13 in which mechanical energy is extracted from this portion of the high pressure feed.
  • the machine 13 expands the vapor substantially isentropically to the operating pressure (approximately 380 psia [2,618 kPa(a)]) of absorbing section 115c, with the work expansion cooling the expanded stream 34a to a temperature of approximately -98°F [-72°C].
  • the partially condensed expanded stream 34a is thereafter supplied as feed to the lower region of absorbing section 115c inside processing assembly 115.
  • Absorbing section 115c contains an absorbing means consisting of a plurality of vertically spaced trays, one or more packed beds, or some combination of trays and packing.
  • the trays and/or packing in absorbing section 115c provide the necessary contact between the vapors rising upward and cold liquid falling downward.
  • the vapor portion of expanded stream 34a rises upward through the absorbing means in absorbing section 115c to be contacted with the cold liquid falling downward to condense and absorb most of the C 3 components and heavier components from these vapors.
  • the liquid portion of expanded stream 34a commingles with liquids falling downward from the absorbing means in absorbing section 115c to form distillation liquid stream 43, which is withdraw from the lower region of absorbing section 115c at -102°F [-74°C].
  • the distillation liquid is heated to -9°F [-23°C] as it cools the vapor portion of stream 32 in separator section 115e as described previously, with the heated distillation liquid stream 43a thereafter supplied to deethanizing section 115d inside processing assembly 115 at an upper mid-column feed point.
  • the flow of this liquid from absorbing section 115c through the heat and mass transfer means in separator section 115e to deethanizing section 115d is via thermosiphon circulation, but a pump could be used.
  • Absorbing section 115c has an internal head or other means to divide it from deethanizing section 115d, so that the two sections inside processing assembly 115 can operate with the pressure of deethanizing section 115d slightly higher than that of absorbing section 115c.
  • This pressure difference provides the driving force that allows a first distillation vapor stream (stream 38) to be withdrawn from the upper region of deethanizing section 115d and directed to the heat exchange means in condensing section 115b inside processing assembly 115.
  • This heat exchange means may likewise be comprised of a fin and tube type heat exchanger, a plate type heat exchanger, a brazed aluminum type heat exchanger, or other type of heat transfer device, including multi-pass and/or multi-service heat exchangers.
  • the heat exchange means is configured to provide heat exchange between first distillation vapor stream 38 flowing through one pass of the heat exchange means and a second distillation vapor stream arising from absorbing section 115c inside processing assembly 115.
  • the second distillation vapor stream is heated while it cools and at least partially condenses stream 38, which thereafter exits the heat exchange means and is separated into its respective vapor and liquid phases.
  • the vapor phase (if any) combines with the heated second distillation vapor stream exiting the heat exchange means to form the residue gas stream that provides cooling in feed cooling section 115a as described previously.
  • the liquid phase is divided into two portions, streams 41 and 42.
  • the first portion (stream 41) is supplied as cold top column feed
  • This absorption cooling effect also facilitates reflux stream 41 condensing and absorbing the C 3 components and heavier components in the distillation vapor flowing upward through absorbing section 115c.
  • the second portion (stream 42) of the liquid phase separated in condensing section 115b is supplied as cold top column feed (reflux) to the upper region of deethanizing section 115d inside processing assembly 115 by gravity flow, so that the cold liquid acts as reflux to absorb and condense the C 3 components and heavier components flowing upward from below so that distillation vapor stream 38 contains minimal quantities of these components.
  • Deethanizing section 115d inside processing assembly 115 contains a mass transfer means consisting of a plurality of vertically spaced trays, one or more packed beds, or some combination of trays and packing.
  • the trays and/or packing in deethanizing section 115d provide the necessary contact between the vapors rising upward and cold liquid falling downward.
  • Deethanizing section 115d also includes a heat and mass transfer means beneath the mass transfer means.
  • This heat and mass transfer means may also be comprised of a fin and tube type heat exchanger, a plate type heat exchanger, a brazed aluminum type heat exchanger, or other type of heat transfer device, including multi-pass and/or multi-service heat exchangers.
  • the heat and mass transfer means is configured to provide heat exchange between a heating medium flowing through one pass of the heat and mass transfer means and a distillation liquid stream flowing downward from the mass transfer means in deethanizing section 115d, so that the distillation liquid stream is heated. As the distillation liquid stream is heated, a portion of it is vaporized to form stripping vapors that rise upward as the remaining liquid continues flowing downward through the heat and mass transfer means.
  • the heat and mass transfer means provides continuous contact between the stripping vapors and the distillation liquid stream so that it also functions to provide mass transfer between the vapor and liquid phases, stripping the liquid product stream 37 of methane, C 2 components, and lighter components.
  • the resulting liquid product (stream 37) exits the lower region of deethanizing section 115d and leaves processing assembly 115 at 203°F [95°C].
  • 115c is warmed in condensing section 115b as it provides cooling to stream 38 as described previously.
  • the warmed second distillation vapor stream combines with any vapor separated from the cooled first distillation vapor stream 38 as described previously.
  • the resulting residue gas stream is heated in feed cooling section 115a as it provides cooling to stream 31 as described previously, whereupon residue gas stream 44 leaves processing assembly 115 at 104°F [40°C].
  • the residue gas stream is then re-compressed in two stages, compressor 14 driven by expansion machine 13 and compressor 20 driven by a supplemental power source. After cooling to 120°F
  • residue gas stream 44c flows to the sales gas pipeline at 915 psia [6,307 kPa(a)], sufficient to meet line requirements (usually on the order of the inlet pressure).
  • the present invention represents more than a 5% improvement over the prior art of the FIG. 1 process.
  • the present invention offers two other advantages over the prior art in addition to the increase in processing efficiency.
  • VOCs volatile organic compounds
  • Some circumstances may favor eliminating feed cooling section 115a and condensing section 115b from processing assembly 115, and using one or more heat exchange means external to the processing assembly for feed cooling and reflux condensing, such as heat exchangers 23 and 17 shown in FIGS. 14 through 21.
  • Such an arrangement allows processing assembly 115 to be smaller, which may reduce the overall plant cost and/or shorten the fabrication schedule in some cases.
  • exchangers 23 and 17 are representative of either a multitude of individual heat exchangers or a single multi-pass heat exchanger, or any combination thereof.
  • Each such heat exchanger may be comprised of a fin and tube type heat exchanger, a plate type heat exchanger, a brazed aluminum type heat exchanger, or other type of heat transfer device, including multi-pass and/or multi-service heat exchangers. In some cases, it may be advantageous to combine the feed cooling and reflux condensing in a single multi-service heat exchanger. With heat exchanger 17 external to the processing assembly, reflux separator 18 and pump 19 will typically be needed to separate condensed liquid stream 40 and deliver at least a portion of it to absorbing section 115c as reflux.
  • the first distillation vapor stream 38 is partially condensed and the resulting condensate used to absorb valuable C 3 components and heavier components from the vapors leaving the work expansion machine.
  • the present invention is not limited to this embodiment. It may be advantageous, for instance, to treat only a portion of the outlet vapor from the work expansion machine in this manner, or to use only a portion of the condensate as an absorbent, in cases where other design considerations indicate portions of the expansion machine outlet or the condensate should bypass absorbing section 115c of processing assembly 115.
  • Feed gas conditions, plant size, available equipment, or other factors may indicate that elimination of work expansion machine 13, or replacement with an alternate expansion device (such as an expansion valve), is feasible, or that total (rather than partial) condensation of first distillation vapor stream 38 in condensing section 115b inside processing assembly 115 (FIGS. 2 through 13) or heat exchanger 17 (FIGS. 14 through 21) is possible or is preferred. It should also be noted that, depending on the composition of the feed gas stream, it may be advantageous to use external refrigeration to provide partial cooling of first distillation vapor stream 38 in condensing section 115b (FIGS. 2 through 13) or heat exchanger 17 (FIGS. 14 through 21).
  • separator 11 can be used to separate cooled first and second portions 32 and 33 into vapor stream 34 and liquid stream 35.
  • separator 11 can be used to separate cooled feed stream 31a into vapor stream 34 and liquid stream 35.
  • FIGS. 4 through 6, 10 through 12, 16, and 20 depict using distillation liquid stream 43 to supply a portion of the cooling of first distillation vapor stream 38 in condensing section 115b (FIGS. 4, 5, 10, and 1 1), heat exchanger 10 (FIGS. 6 and 12), or heat exchanger 17 (FIGS. 16 and 20).
  • a heat and mass transfer means may not be needed in separator section 115e (FIGS. 4 through 6 and 16) or separator 11 (FIGS. 10 through 12 and 20).
  • a pump 22 is used to deliver distillation liquid stream 43 to the heat exchange means in condensing section 115b.
  • condensing section 115b is located below absorbing section 115c in processing assembly 115 so that flow of distillation liquid stream 43 is via thermosiphon circulation.
  • a heat exchanger 10 external to processing assembly 115 is employed and feed cooling section 115a is located below absorbing section 115c in processing assembly 115 so that flow of distillation liquid stream 43 is via thermosiphon circulation.
  • the embodiments shown in FIGS. 5, 6, 1 1 , and 12 use reflux pump 19 to supply reflux to locations above the point in processing assembly 115 where the liquid phase condensed from stream 38 is collected.)
  • FIGS. 5 In the embodiments shown in FIGS.
  • thermosiphon circulation may be sufficient to allow distillation liquid stream 43 to flow through heat exchanger 17, or pump 22 may be needed to circulate stream 43.
  • Some circumstances may favor using distillation liquid stream 43 to cool stream 32 in a heat exchanger external to processing assembly 115, such as heat exchanger 10 depicted in FIGS. 3, 9, 15, and 19. Still other circumstances may favor no heating of distillation liquid stream 43 at all, and instead using distillation liquid stream 43 as the reflux to the upper region of deethanizing section 115d as shown in FIGS. 7, 13, 17, and 21 . (For the embodiment shown in FIGS.
  • the cooled first and second portions 32 and 33 entering separator section 115e in FIGS. 2 and 14 or separator 11 in FIGS. 8 and 18 may not contain any liquid (because it is above its dewpoint, or because it is above its cricondenbar). In such cases, there is no liquid in stream 35 (as shown by the dashed lines). In such circumstances, separator section 115e in processing assembly 115 (FIGS. 2 through 7 and 14 through 17) or separator 11 (FIGS. 8 through 13 and 18 through 21) may not be required.
  • the use of external refrigeration to supplement the cooling available to the inlet gas and/or the first distillation vapor stream from the second distillation vapor stream and the distillation liquid stream may be employed, particularly in the case of a rich inlet gas.
  • a heat and mass transfer means may be included in separator section 115e (or a gas collecting means in such cases when the cooled first and second portions 32 and 33 or the cooled feed stream 31a contains no liquid) as shown by the dashed lines in FIGS. 3 through 7 and 15 through 17, or a heat and mass transfer means may be included in separator 11 as shown by the dashed lines in FIGS. 9 though 13 and 19 through 21.
  • This heat and mass transfer means may be comprised of a fin and tube type heat exchanger, a plate type heat exchanger, a brazed aluminum type heat exchanger, or other type of heat transfer device, including multi-pass and/or multi-service heat exchangers.
  • the heat and mass transfer means is configured to provide heat exchange between a refrigerant stream (e.g., propane) flowing through one pass of the heat and mass transfer means and the vapor portion of stream 31a flowing upward, so that the refrigerant further cools the vapor and condenses additional liquid, which falls downward to become part of the liquid removed in stream 35.
  • a refrigerant stream e.g., propane
  • separator 11 may include provisions for providing supplemental cooling with refrigerant.
  • conventional gas chiller(s) could be used to cool stream 32, stream 33, and/or stream 31a with refrigerant before streams 32 and 33 enter separator section 115e (FIGS. 2 and 14) or separator 11 (FIGS. 8 and 18) or stream 31a enters separator section 115e (FIGS. 3 through 7 and 15 through 17) or separator 11 (FIGS. 9 through 13 and 19 through 21).
  • the heat exchange means in condensing section 115b of processing assembly 115 (FIGS. 2 through 5, 7 through 11, and 13), heat exchanger 10 (FIGS. 6 and 12), or heat exchanger 17 (FIGS. 14 through 21) may include provisions for providing supplemental cooling with refrigerant as shown by the dashed lines.
  • the multi-pass and/or multi-service heat transfer device will include appropriate means for distributing, segregating, and collecting stream 31, stream 32, stream 33, first distillation vapor stream 38, any vapor separated from the cooled stream 38, and the second distillation vapor stream in order to accomplish the desired cooling and heating.
  • the present invention provides improved recovery of C 3 components and heavier hydrocarbon components per amount of utility consumption required to operate the process.
  • An improvement in utility consumption required for operating the process may appear in the form of reduced power requirements for compression or re-compression, reduced power requirements for external refrigeration, reduced energy requirements for tower reboiling, or a combination thereof.

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  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
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  • Separation By Low-Temperature Treatments (AREA)
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Abstract

Procédé et appareil pour ensemble de traitement compact permettant de récupérer le propane, le propylène, et autres composants hydrocarbonés lourds contenus dans un flux gazeux hydrocarboné. Le flux gazeux est refroidi, dilaté à une pression plus basse, et introduit dans un moyen d'absorption. Un premier flux de liquide de distillation provenant du moyen d'absorption est appliqué à un moyen de transfert de masse. Un premier flux de vapeur de distillation provenant du moyen de transfert de masse est refroidi pour le condenser partiellement, et former un flux de vapeur résiduaire et un flux condensé. Le flux condensé est introduit, à titre de charge par le haut, dans le moyen d'absorption. Un second flux de vapeur de distillation provenant du moyen d'absorption est chauffé par refroidissement du premier flux de vapeur de distillation, combiné au flux de vapeur résiduaire, et chauffé par refroidissement du flux gazeux. Un second flux de liquide de distillation provenant du moyen de transfert de masse est chauffé dans un moyen de transfert de chaleur et de masse pour éliminer par entraînement les composants volatils qu'il contient.
EP11766369A 2010-03-31 2011-03-18 Traitement des gaz hydrocarbonés Withdrawn EP2553367A1 (fr)

Applications Claiming Priority (7)

Application Number Priority Date Filing Date Title
PCT/US2010/029331 WO2010144172A1 (fr) 2009-06-11 2010-03-31 Traitement de gaz d'hydrocarbures
US12/750,862 US8881549B2 (en) 2009-02-17 2010-03-31 Hydrocarbon gas processing
US12/772,472 US9933207B2 (en) 2009-02-17 2010-05-03 Hydrocarbon gas processing
US12/781,259 US9939195B2 (en) 2009-02-17 2010-05-17 Hydrocarbon gas processing including a single equipment item processing assembly
US13/048,315 US9052136B2 (en) 2010-03-31 2011-03-15 Hydrocarbon gas processing
US13/051,682 US9074814B2 (en) 2010-03-31 2011-03-18 Hydrocarbon gas processing
PCT/US2011/029034 WO2011126710A1 (fr) 2010-03-31 2011-03-18 Traitement des gaz hydrocarbonés

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CN (1) CN102472574B (fr)
AU (1) AU2011238799B2 (fr)
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CO (1) CO6480968A2 (fr)
EA (1) EA023918B1 (fr)
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US5675054A (en) * 1995-07-17 1997-10-07 Manley; David Low cost thermal coupling in ethylene recovery
US5685170A (en) * 1995-11-03 1997-11-11 Mcdermott Engineers & Constructors (Canada) Ltd. Propane recovery process
US7310971B2 (en) * 2004-10-25 2007-12-25 Conocophillips Company LNG system employing optimized heat exchangers to provide liquid reflux stream
US6516631B1 (en) * 2001-08-10 2003-02-11 Mark A. Trebble Hydrocarbon gas processing
US6694775B1 (en) * 2002-12-12 2004-02-24 Air Products And Chemicals, Inc. Process and apparatus for the recovery of krypton and/or xenon
US7484385B2 (en) * 2003-01-16 2009-02-03 Lummus Technology Inc. Multiple reflux stream hydrocarbon recovery process
CA2515999C (fr) * 2003-02-25 2012-12-18 Ortloff Engineers, Ltd. Traitement des hydrocarbures gazeux
US8919148B2 (en) * 2007-10-18 2014-12-30 Ortloff Engineers, Ltd. Hydrocarbon gas processing
EP2440867A4 (fr) * 2009-06-11 2018-04-18 Ortloff Engineers, Ltd Traitement de gaz d'hydrocarbures

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CO6480968A2 (es) 2012-07-16
CN102472574B (zh) 2015-05-13
CN102472574A (zh) 2012-05-23
JP2013524149A (ja) 2013-06-17
CA2764579C (fr) 2016-10-11
CA2764579A1 (fr) 2011-10-13
EA023918B1 (ru) 2016-07-29
MY160268A (en) 2017-02-28
AU2011238799B2 (en) 2016-01-14
JP5870085B2 (ja) 2016-02-24
AU2011238799A1 (en) 2012-02-02
WO2011126710A1 (fr) 2011-10-13

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