EP2440867A1 - Traitement de gaz d'hydrocarbures - Google Patents

Traitement de gaz d'hydrocarbures

Info

Publication number
EP2440867A1
EP2440867A1 EP10786524A EP10786524A EP2440867A1 EP 2440867 A1 EP2440867 A1 EP 2440867A1 EP 10786524 A EP10786524 A EP 10786524A EP 10786524 A EP10786524 A EP 10786524A EP 2440867 A1 EP2440867 A1 EP 2440867A1
Authority
EP
European Patent Office
Prior art keywords
stream
receive
mass transfer
processing assembly
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Withdrawn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
EP10786524A
Other languages
German (de)
English (en)
Other versions
EP2440867A4 (fr
Inventor
Andrew F. Johnke
W. Larry Lewis
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.)
Honeywell UOP LLC
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
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=56291166&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=EP2440867(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Priority claimed from US12/689,616 external-priority patent/US9021831B2/en
Priority claimed from US12/717,394 external-priority patent/US9080811B2/en
Application filed by Ortloff Engineers Ltd, SME Products LP filed Critical Ortloff Engineers Ltd
Publication of EP2440867A1 publication Critical patent/EP2440867A1/fr
Publication of EP2440867A4 publication Critical patent/EP2440867A4/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • 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
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • 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
    • F25J3/0204—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
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • 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
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins
    • 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
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/78—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
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/12—Refinery or petrochemical off-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
    • 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
    • F25J2270/12—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.
    • 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
    • F25J2290/42—Modularity, pre-fabrication of modules, assembling and erection, horizontal layout, i.e. plot plan, and vertical arrangement of parts of the cryogenic unit, e.g. of the cold box
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/20—Capture or disposal of greenhouse gases of methane

Definitions

  • This invention relates to a process and apparatus for the separation of a gas containing hydrocarbons.
  • the applicants claim the benefits under Title 35, United States Code, Section 119(e) of prior U.S. Provisional Application Number 61/186,361 which was filed on June 11, 2009.
  • the applicants also claim the benefits under Title 35, United States Code, Section 120 as a continuation-in-part of U.S. Patent Application No. 12/717,394 which was filed on March 4, 2010, and as a continuation-in-part of U.S. Patent Application No. 12/689,616 which was filed on January 19, 2010, and as a continuation-in-part of U.S. Patent Application No. 12/372,604 which was filed on February 17, 2009.
  • Assignees S.M.E. Products LP and Ortloff Engineers, Ltd. were parties to a joint research agreement that was in effect before the invention of this application was made.
  • 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.
  • cryogenic processes have become popular because of the availability of economical equipment that produces power while simultaneously expanding and extracting heat from the gas being processed.
  • the richness (ethane, ethylene, and heavier hydrocarbons content) of the gas, and the desired end products may be employed.
  • Patent No. 33,408; and co-pending application nos. 11/430,412; 11/839,693; 11/971,491; and 12/206,230 describe relevant processes (although the description of the present invention in some cases is based on different processing conditions than those described in the cited U.S. Patents).
  • 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 feed gas is not totally condensed (typically it is not)
  • 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 separation that takes place in this process consumes energy for feed gas cooling, for reboiling the deethanizing section, for refluxing the absorbing section, and/or for re-compressing the residue gas.
  • the present invention employs a novel means of performing the various steps described above more efficiently and using fewer pieces of equipment.
  • 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.
  • VOCs volatile organic compounds
  • eliminating these flanges reduces the potential for atmospheric emissions that can damage the environment.
  • C 3 recoveries in excess of 99.6% can be obtained while providing essentially complete rejection of C 2 components to the residue gas stream.
  • the present invention makes possible essentially 100% separation of C 2 components and lighter components from the C 3 components and heavier components at lower energy requirements compared to the prior art while maintaining the same recovery level.
  • the present invention although applicable at lower pressures and warmer temperatures, is particularly advantageous when processing feed gases in the range of
  • 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 13 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 0 F [43°C] and 885 psia [6,100 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.
  • 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 0 F [-76 0 C] (stream 43).
  • the cooled stream 31a enters separator 11 at -34°F [-36 0 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 [2,583 kPa(a)]) of fractionation tower 15 by expansion valve 12, cooling stream 35a to -65 0 F [-54 0 C].
  • Stream 35a enters heat exchanger 10 to supply cooling to the feed gas as described previously, heating stream 35b to 105 0 F [41 0 C] before it is supplied to fractionation tower 15 at a lower mid-column feed point.
  • 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 0 F [-74 0 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.
  • the vapor portion of expanded stream 34a rises upward through absorbing section 15a and is contacted with cold liquid falling downward to condense and absorb the C 3 components and heavier components.
  • 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 0 F [-79 0 C].
  • the cold deethanizer overhead stream is warmed to approximately -33 0 F [-66 0 C] (stream 36a) as it cools stream 38 from -30 0 F [-35 0 C] to about -103 0 F [-75 0 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 0 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. 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 0 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 0 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 (usually on the order of the inlet pressure).
  • 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 0 C], while the remaining second portion (stream 33) is further cooled so that it leaves the heat exchange means at -20 0 F [-29 0 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. [0031]
  • the second portion (stream 33) of stream 31 enters separator section
  • any condensed liquid is separated from the vapor and commingles with any liquid that is condensed from the vapor portion of stream 32 flowing up through the heat and mass transfer means.
  • the vapor portion of stream 33 combines with the vapor leaving the heat and mass transfer means to form stream 34, which exits separator section 115e at -31 0 F [-35 0 C].
  • the liquid portions (if any) of streams 32 and 33 and any liquid condensed from the vapor portion of stream 32 in the heat and mass transfer means combine to form stream 35, which exits separator section 115e at -15 0 F [-26 0 C].
  • 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 0 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 0 F [-74 0 C].
  • the distillation liquid is heated to -9°F [-23 0 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. [0035]
  • 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 0 F [95 0 C]. [0037]
  • residue gas stream 44c 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 0 F [40 0 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 0 F [49°C] in discharge cooler 21, 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 offers two other advantages over the prior art in addition to the increase in processing efficiency.
  • the compact arrangement of processing assembly 115 of the present invention replaces six separate equipment items in the prior art (heat exchangers 10 and 17, separator 11, reflux separator 18, reflux pump 19, and fractionation tower 15 in FIG. 1) with a single equipment item (processing assembly 115 in FIG. T). This reduces the plot space requirements, eliminates the interconnecting piping, and eliminates the power consumed by the reflux pump, reducing the capital cost and operating cost of a process plant utilizing the present invention over that of the prior art.
  • VOCs volatile organic compounds
  • 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 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.
  • 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 and 10 through 12 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 11) or heat exchanger 10 (FIGS. 6 and 12).
  • a heat and mass transfer means may not be needed in separator section 115e (FIGS. 4 through 6) or separator 11 (FIGS. 10 through 12).
  • 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.
  • reflux pump 19 uses 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.
  • 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 and 9. 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 and 13. (For the embodiment shown in FIG. 13, pump 22 may be needed because gravity flow of stream 43 may not be possible.)
  • the cooled first and second portions 32 and 33 entering separator section 115e in FIG. 2 or separator 11 in FIG. 8 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) or separator 11 (FIGS. 8 through 13) 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 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, or a heat and mass transfer means may be included in separator 11 as shown by the dashed lines in FIGS. 9 though 13.
  • 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 section 115e FIG. 2
  • separator 11 separator 11
  • the heat exchange means in condensing section 115b of processing assembly 115 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)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Separation By Low-Temperature Treatments (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un procédé et un dispositif permettant de récupérer du propane, du propylène et des composants hydrocarbonés plus lourds à partir d'un flux gazeux hydrocarboné dans un ensemble de traitement compact. Le flux gazeux est refroidi, dilaté à une pression inférieure et fourni comme charge de fond à des moyens d'absorption prévus dans l'ensemble de traitement. Un premier flux liquide de distillation est collecté à partir de la région inférieure des moyens d'absorption et fourni comme charge supérieure à des moyens de transfert de masse prévus dans l'ensemble de traitement. Un premier flux de vapeur de distillation est collecté à partir de la région supérieure des moyens de transfert de masse et refroidi suffisamment pour être au moins partiellement condensé, de manière à former un flux de vapeur résiduel et un flux condensé. Le flux condensé est fourni comme charge supérieure des moyens d'absorption. Un deuxième flux de vapeur de distillation est collecté à partir de la région supérieure des moyens d'absorption et dirigé dans un ou plusieurs moyens d'échange de chaleur prévus dans l'ensemble de traitement afin d'être chauffé, pendant que le premier flux de vapeur de distillation est refroidi. Le deuxième flux de vapeur de distillation est combiné à n'importe quel flux de vapeur résiduel, et le flux combiné est dirigé dans un ou plusieurs moyens d'échange de chaleur prévus dans l'ensemble de traitement afin d'être chauffé pendant que le flux gazeux est refroidi. Un deuxième flux liquide de distillation est collecté à partir de la région inférieure des moyens de transfert de masse et dirigé dans des moyens de transfert de chaleur et de masse prévus dans l'ensemble de traitement afin d'être chauffé et d'en extraire les composants volatils. Les quantités et les températures des charges appliquées aux moyens d'absorption permettent de maintenir la température de la région supérieure des moyens d'absorption à une température à laquelle la majeur partie des constituants voulus sont récupérés dans le deuxième flux liquide de distillation épuisé.
EP10786524.8A 2009-06-11 2010-03-31 Traitement de gaz d'hydrocarbures Withdrawn EP2440867A4 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US18636109P 2009-06-11 2009-06-11
US12/689,616 US9021831B2 (en) 2009-02-17 2010-01-19 Hydrocarbon gas processing
US12/717,394 US9080811B2 (en) 2009-02-17 2010-03-04 Hydrocarbon gas processing
PCT/US2010/029331 WO2010144172A1 (fr) 2009-06-11 2010-03-31 Traitement de gaz d'hydrocarbures

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MY160268A (en) * 2010-03-31 2017-02-28 Ortloff Engineers Ltd Hydrocarbon gas processing
MY179078A (en) * 2013-09-11 2020-10-27 Ortloff Engineers Ltd Hydrocarbon gas processing
MX363766B (es) * 2013-12-06 2019-04-02 Exxonmobil Upstream Res Co Metodo y dispositivo para separar hidrocarburos y contaminantes con un mecanismo de calentamiento para desestabilizar y/o prevenir la adhesion de solidos.

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JPS546500B1 (fr) * 1976-02-15 1979-03-29
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WO2005114076A1 (fr) * 2004-04-26 2005-12-01 Ortloff Engineers, Ltd Liquefaction de gaz naturel
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MY161443A (en) 2017-04-14
EA025641B1 (ru) 2017-01-30
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AU2010259245A2 (en) 2012-05-10
CA2764282C (fr) 2016-01-05
JP5552160B2 (ja) 2014-07-16
EA201270003A1 (ru) 2012-07-30
WO2010144172A1 (fr) 2010-12-16
KR20120028359A (ko) 2012-03-22
EP2440867A4 (fr) 2018-04-18
AR076383A1 (es) 2011-06-08
CN102803881B (zh) 2015-08-19
CO6480937A2 (es) 2012-07-16
PE20121402A1 (es) 2012-10-26
CN102803881A (zh) 2012-11-28
KR101680922B1 (ko) 2016-11-29
MX2011013071A (es) 2012-02-01
AU2010259245B2 (en) 2016-09-29
AU2010259245A1 (en) 2012-02-23

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