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WO2010141996A1 - Dispositif et procédé pour séparer un gaz acide en gaz adouci et liquide acide - Google Patents

Dispositif et procédé pour séparer un gaz acide en gaz adouci et liquide acide Download PDF

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Publication number
WO2010141996A1
WO2010141996A1 PCT/AU2010/000723 AU2010000723W WO2010141996A1 WO 2010141996 A1 WO2010141996 A1 WO 2010141996A1 AU 2010000723 W AU2010000723 W AU 2010000723W WO 2010141996 A1 WO2010141996 A1 WO 2010141996A1
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WO
WIPO (PCT)
Prior art keywords
sour
liquid
collection zone
separator vessel
hydrocarbon
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.)
Ceased
Application number
PCT/AU2010/000723
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English (en)
Inventor
Nimalan Gnanendran
Martin Wilkes
Simon Elliot
Allan Hart
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.)
Cool Energy Ltd
Original Assignee
Cool Energy Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from AU2009902743A external-priority patent/AU2009902743A0/en
Application filed by Cool Energy Ltd filed Critical Cool Energy Ltd
Publication of WO2010141996A1 publication Critical patent/WO2010141996A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/061—Natural gas or substitute natural gas
    • 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
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0635—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the 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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/064—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the 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
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/067—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0695—Start-up or control of the process; Details of the apparatus used
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/06—Polluted air
    • 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
    • F25J2205/20—Processes or apparatus using other separation and/or other processing means using solidification of components
    • 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
    • F25J2210/66—Landfill or fermentation off-gas, e.g. "Bio-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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
    • F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
    • 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/80—Integration in an installation using carbon dioxide, e.g. for EOR, sequestration, refrigeration 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
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/02—Control in general, load changes, different modes ("runs"), measurements
    • 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
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the present invention relates to an apparatus and process for separating a sour gas into sweetened gas and sour liquid.
  • liquid level control is relatively easy to manage.
  • the liquid level within the separator can be allowed to fluctuate quite widely without compromising vapour-liquid separation because controlling the pressure conditions within the vessel will maintain steady state equilibrium as the liquid level within the vessel changes .
  • Liquid level control is much more difficult in a multiphase process separator in which vapour, one or more liquids, and solids are formed and co-exist.
  • the management of solids is particularly problematic.
  • solids may form and accumulate on the walls of the separator.
  • Periodic accumulation of solids in the vapour space of the separator followed by sudden bulk entry of solids into the liquid phase will have the effect of disrupting the liquid level within the separator.
  • the temperature of the liquid phase lies above the melting point of the solids collected within the liquid phase, the temperature of the liquid phase will also change due to the release of latent heat from the melting solids.
  • the natural gas stream is cooled to temperatures at which carbon dioxide (and other sour contaminants and freezable hydrocarbon components) condense and/or solidify to produce a slurry of solid sour contaminants in a hydrocarbon liquid and a sweetened vapour stream.
  • the solid contaminants may be preferably melted before removing the contaminant stream from the separator as a liquid. Melting of such solids is generally facilitated by introducing a heater into the portion of the separator where the slurry collects. Therefore, the liquid phase in the separator may be at a higher temperature than the vapour phase.
  • the ability to control temperature equilibrium conditions within such a separator is much more complex than in a two-phase vapour- liquid separator. The inventors have realised after substantial field testing that the ability to control the liquid level is inter-related to heater control within the separator and is therefore very important in this regard.
  • any solids formed in the vapour space will fall through the colder upper layer before they are melted in the lower layer, making control of the interface difficult, due to the thermal perturbations in the vicinity of the interface.
  • the present invention seeks to overcome at least some of the aforementioned disadvantages.
  • the invention provides an apparatus and process for separating a sour gas into sweetened gas and sour liquids.
  • the apparatus is adapted to control a level of sour liquid in the separator vessel while ⁇ maintaining a steady melting and removal of the solid species .
  • an apparatus for separating a sour gas stream into sweetened gas and sour liquid comprising: a separator vessel having a vapour space and a sour liquid collection zone; a means for introducing the sour gas stream into the vapour space, the vapour space being arranged to operate under conditions whereby introducing the sour gas stream into the vapour space produces a mixture of sour liquid and/or solids, hydrocarbon vapour and, optionally, hydrocarbon liquid, the sour liquid and/or solids and the hydrocarbon liquid, if present, separating under gravity and density to the sour liquid collection zone, thereby producing sweetened gas in the vapour space ; a heating means in the sour liquid collection zone for melting sour solids that collect in the sour liquid collection zone into sour liquid; an outlet for withdrawing sweetened gas from the vapour space ; an outlet for withdrawing sour liquid from the sour liquid collection zone; and means for controlling a level
  • said means controls the sour liquid at a desired level in the separator vessel.
  • the sour liquid in the sour liquid collection zone may be maintained at a higher temperature than the vapour space to melt solids which collect in the sour liquid collection zone.
  • the temperature of the sour liquid may be therefore largely controlled by controlling operation of the heater.
  • the inventors have realized that maintaining temperature control in the sour liquid collection zone is also facilitated by maintaining stable control of the liquid level in the apparatus .
  • means for controlling the liquid level in the separator vessel comprises a non-stick surface provided on interior wall(s) of the separator vessel.
  • the non-stick surface may extend continuously on the entire interior wall(s) of the separator vessel or may extend substantially over the interior wall(s) of the separator vessel disposed in the vapour space therein.
  • Such non-stick surfaces may be provided by coating or lining a surface of the separator vessel with a material capable of preventing solid accumulation on the separator vessel walls.
  • suitable materials includes, but is not limited to, TeflonTM.
  • the means for controlling the liquid level in the separator vessel comprises a liquid level control valve assembly in fluid communication with the outlet in the sour liquid collection zone.
  • the liquid level control valve assembly maintains the liquid level at the desired level in the separator vessel .
  • a two phase liquid- liquid interface between a denser, warmer CO 2 -rich stream and a lighter, colder hydrocarbon-rich liquid stream may be established within a separator vessel, and it is important to not only control the liquid level within the separator vessel but to maintain a substantially stable interface between the hydrocarbon liquid and the sour liquid in the separator vessel .
  • an apparatus for separating a sour gas stream into sweetened gas, liquid hydrocarbon, and sour liquid comprising: a separator vessel having an upper vapour space, a lower sour liquid collection zone, and an upper hydrocarbon liquid collection zone disposed between the upper vapour space and the lower sour liquid collection zone; a means for introducing the sour gas stream into the upper vapour space, the upper vapour space being arranged to operate under conditions whereby introducing the sour gas stream into the upper vapour space produces a mixture of sour liquid and/or solids, hydrocarbon vapour and hydrocarbon liquid, the sour liquid and/or solids and the hydrocarbon liquid separating under gravity and density to the lower sour liquid collection zone and the upper hydrocarbon liquid collection zone, respectively, thereby producing sweetened gas in the upper vapour space ; a heating means in the lower sour liquid collection zone for melting sour solids that collect in the lower sour liquid collection zone into sour liquid;
  • substantially stable interface refers to a substantially continuous horizontal boundary between an upper hydrocarbon rich liquid phase and a lower sour liquid rich phase which are distinguished by their density and temperature. It will be appreciated that the sour liquid and hydrocarbon liquid have a degree of mutual solubility and therefore the horizontal boundary between the upper and lower liquid phases will comprise a transition region whose thickness will vary according to thermodynamic and kinetic parameters known to those skilled in the art, as well as temperature and pressure conditions in the separator vessel .
  • the means for introducing the sour gas stream into the upper vapour space may comprise an inlet in the upper vapour space of the separation vessel.
  • a gas expansion device defines the inlet of the upper vapour space. Suitable examples of such gas expansion devices include, but are not limited to, Joule-Thomson valves, venturi devices, turbo expanders, and so forth.
  • the means for introducing the sour gas stream into the upper vapour space may further comprise means to introduce the sour gas stream into the upper vapour space with a spiral flow to aid separation of the mixture of sour liquid and/or solids, methane vapour and hydrocarbon liquid produced in the upper vapour space.
  • the means may comprise other suitable separation means.
  • the heating means is a heater, in particular an immersion heater.
  • the means for maintaining a substantially stable interface between the hydrocarbon liquid and the sour liquid in the separator vessel comprises a first level control valve assembly in fluid communication with the outlet in the lower sour liquid collection zone and a second level control valve assembly in fluid communication with the outlet in the upper hydrocarbon liquid collection zone.
  • the first and second level control assemblies maintain the substantially stable interface between the hydrocarbon liquid and the sour liquid at the desired level in the separator vessel.
  • first and second level control assemblies also maintain a substantially stable interface between the upper vapour space and the upper hydrocarbon liquid phase.
  • the first and second level control assemblies maintain the substantially stable interface between the upper vapour space and the upper hydrocarbon liquid phase at a desired level in the separator vessel. It will be appreciated that the apparatus of the present invention is operated under conditions where solid particles of sour species form in the vapour space and migrate downwardly through the upper hydrocarbon liquid phase before reaching the lower sour species liquid phase.
  • the movement of solids through the liquid phases makes it difficult to accurately determine the location of the liquid-liquid interface in the vessel because the determination of the location of the interface in the vessel is typically conducted by sensing the density of each of the phases (for example by using ultrasonic measurements) and the falling solids interfere with the measurements and/or provide false readings.
  • the movement of solids through the liquid phases also disturbs the interface therebetween.
  • the first and second level control valve assemblies may be operatively controlled in response to signals received from one or more probes and/or sensors disposed in the lower sour liquid collection zone and/or the upper hydrocarbon liquid collection zone.
  • the probes and/or sensors are arranged in use to measure one or more of physical parameters within the respective liquid phases which remain relatively unaffected by falling solids in the liquid phases. Suitable examples of such physical parameters include, but are not limited to, differential temperature, RF capacitance, and so forth, as will be known to persons skilled in the art.
  • the control valve assemblies may also be operatively controlled in response to signals from sensors disposed in the upper vapour space of the vessel .
  • hydrocarbon liquid may become entrained in the sour liquid collected in the lower sour liquid collection zone.
  • the temperature of the sour liquid in the sour liquid collection zone, and particularly proximal to the heating means is likely to be greater than the boiling point of the hydrocarbon liquid, the entrained hydrocarbon liquid may be re-vapourised in the sour liquid collection zone and/or proximal to the heating means.
  • hydrocarbon vapour bubbles may be generated and rise through the sour liquid. If allowed to rise freely these vapour bubbles will disturb the interface between the sour liquid and hydrocarbon liquid phases, cause undesired mixing and turbulence between the sour liquid and hydrocarbon liquid phases, and interfere with the settling of solids through the upper hydrocarbon liquid phase. Further, bubbling might also cause change in physical properties, such as density, causing the level transmitters to indicate unsteady readings, which in turn might lead to an unsteady process operation.
  • the means for maintaining a substantially stable interface between the hydrocarbon liquid and the sour liquid in the separator vessel further comprises means for directing vapour generated in the sour liquid collection zone to the upper vapour space.
  • the directing means is configured to minimise disturbance of the vapour-liquid interface and/or liquid-liquid interace.
  • the directing means comprises a riser assembly to facilitate fluid communication between the lower sour liquid collection zone and the upper vapour space.
  • the riser assembly comprises a vertical component extending upwardly from a lower conical component, the lower conical component being disposed in the sour liquid collection zone and the vertical component extending through the hydrocarbon liquid collection zone and terminating in the upper vapour space of the separator vessel.
  • the lower conical component is disposed above and proximal to the heating means. Hydrocarbon vapour generated from entrained hydrocarbons in the sour liquid collection zone enters the conical component and passes upwardly through the conical component and the vertical component and exits the vertical component in the upper vapour space without encountering the upper liquid layer.
  • the riser assembly may be formed from material having low thermal conductivity.
  • the riser assembly is provided with nonstick surfaces and downward sloping surfaces to prevent falling solids from accumulating thereon.
  • the vertical component may be configured to prevent sour solids from entering from the top.
  • the vertical component is provided with a cap having downwardly inclined surfaces.
  • the cap may be configured to expel hydrocarbon vapour substantially laterally into the upper vapour space .
  • the separator vessel is provided with an inlet disposed in the lower sour liquid collection zone, wherein the inlet is configured to introduce sour liquid into the lower sour liquid collection zone.
  • This particular feature may be useful to facilitate establishment of two distinct liquid layers in the separator vessel, particularly during start up operations.
  • a process for separating a sour gas stream into sweetened gas, liquid hydrocarbon, and sour liquid comprising the steps of: introducing the sour gas stream into an upper vapour space of a separator vessel operated under conditions to produce a mixture of sour liquid and/or solids, hydrocarbon vapour and hydrocarbon liquid in the upper vapour space; allowing the sour liquids and/or solids and the hydrocarbon liquid to separate under gravity and density to a lower sour liquid collection zone and an upper hydrocarbon liquid collection zone provided in the separator vessel, respectively, thereby producing a sweetened gas in the upper vapour space ; melting sour solids that collect in the lower sour liquid collection zone into sour liquid; withdrawing sweetened gas from the upper vapour space; withdrawing hydrocarbon liquid from the upper hydrocarbon liquid collection zone; and withdrawing sour liquid from the lower sour liquid collection zone; wherein the step of withdrawing the hydrocarbon liquid and/or the step of withdrawing the sour liquid
  • the step of withdrawing the sour liquid is performed in a manner to maintain the substantially stable interface between the hydrocarbon liquid and the sour liquid at a desired level in the separator vessel.
  • the step of withdrawing the sour liquid is performed in a manner to maintain a substantially stable interface between the upper vapour space and the upper hydrocarbon liquid phase. In a preferred embodiment, the step of withdrawing the sour liquid is performed in a manner to maintain the substantially stable interface between the upper vapour space and the upper hydrocarbon liquid phase at a desired level in the separator vessel.
  • the process comprises heating the sour solids to a temperature at or just above the melting point of the sour solids.
  • the step of withdrawing the hydrocarbon liquid and/or the step of withdrawing the sour liquid comprises controllably withdrawing the hydrocarbon liquid and/or the sour liquid with respective first and second level control valve assemblies in response to signals received from one or more probes and/or sensors disposed in the lower sour liquid collection zone and/or the upper hydrocarbon liquid collection zone and/or the upper vapour space of the separator vessel for determining the interface .
  • the separator vessel is operated under a set of temperature and pressure conditions at which the sour species solidifies and/or a liquid condensate of sour species forms. It will be appreciated that the set of temperature and pressure conditions will vary in accordance with the desired composition of the product gas stream.
  • the sour gas stream is cooled prior to introduction to the upper vapour space of the separator vessel to a temperature at or just below the temperature at which the sour species solidifies and/or condenses.
  • the step of cooling the sour gas stream comprises cooling and expanding the sour gas stream in one or more expansion steps.
  • the step of cooling the gas stream comprises effecting a direct heat exchange with a cooling stream.
  • the sour gas stream may be pre- cooled to a temperature just above the temperature at which the sour species solidifies and/or condenses prior to introducing the sour gas stream into the separator vessel.
  • Figure 1 shows a schematic diagram of an apparatus for separating a sour gas stream into sweetened gas and sour liquid in accordance with one embodiment of the present invention
  • Figure 2 shows a schematic diagram of an alternative embodiment of the apparatus shown in Figure 1 ; and Figure 3 shows a schematic diagram of an apparatus for separating a sour gas stream into sweetened gas and sour liquid in accordance with a further embodiment of the present invention.
  • an apparatus 10 for separating a sour gas stream into sweetened gas, liquid hydrocarbon, and sour liquid there is shown an apparatus 10 for separating a sour gas stream into sweetened gas, liquid hydrocarbon, and sour liquid.
  • the apparatus 10 includes a separator vessel 12 having an upper vapour space 14, a lower sour liquid collection zone 16, and an upper hydrocarbon liquid collection zone 18 disposed between the upper vapour space 14 and the lower sour liquid collection zone 16.
  • a reference to a hydrocarbon liquid may encompass a "rich hydrocarbon liquid” comprising a mixture of one or more condensable hydrocarbons and one or more sour or other components.
  • a reference to a sour liquid may encompass a rich sour liquid comprising a mixture of one or more sour contaminants and one or more hydrocarbons.
  • the wt% of hydrocarbons is greater than the sour components in a rich hydrocarbon liquid, and conversely the wt% of sour components is greater than the hydrocarbon components in a rich sour liquid.
  • the interior walls of the separator vessel 12 are provided with a non-stick surface.
  • the non-stick surface may extend continuously on the entire interior wall(s) of the separator vessel 12 or may extend substantially over the interior wall(s) of the separator vessel 12 disposed in the vapour space 14 therein.
  • Such non-stick surfaces may be provided by coating or lining a surface of the separator vessel 12 with a material capable of preventing solids accumulation on the separator vessel walls.
  • suitable materials includes, but is not limited to, TeflonTM.
  • TeflonTM TeflonTM
  • the separator vessel 12 is provided with an inlet 20 for introducing a sour gas into the upper vapour space 14, an outlet 22 for withdrawing sweetened gas from the upper vapour space 14, an outlet 24 for withdrawing hydrocarbon liquid from the upper hydrocarbon liquid collection zone 18, and an outlet 26 for withdrawing sour liquid from the lower sour liquid collection zone 16.
  • the upper vapour space 14 of the separator vessel 12 is arranged to operate under conditions whereby introducing the sour gas stream into the upper vapour space 14 produces a mixture of sour liquid and/or solids, methane vapour and hydrocarbon liquid.
  • the sour gas stream is cooled on introduction to the upper vapour space 14 of the separator vessel 12 to a temperature at or just below the temperature at which the sour species in the sour gas stream solidifies and/or condenses. It will be appreciated that the operating temperature and pressure of the separator vessel 12 will vary in accordance with the desired composition of the sweetened gas stream.
  • the inlet 20 may be defined by a gas expansion device 28.
  • the gas expansion device is a Joule- Thomson valve, but alternative suitable examples of gas expansion devices 28 include venturi devices, turbo expanders , and so forth .
  • the inlet 20 may also include an inlet device to assist or enhance separation of liquid and/or solid sour species and liquid hydrocarbon from the mixture formed in the upper vapour space 14.
  • Some inlet devices are designed to coalesce droplets or agglomerate solid particles.
  • Other inlet devices are configured to introduce the sour gas stream into the upper vapour space 14 with a swirl to aid separation of the mixture of sour liquid and/or solids, methane vapour and hydrocarbon liquid produced in the upper vapour space 14.
  • the separator vessel 12 is also provided with a heating means 30 disposed in the lower sour liquid collection zone 16 for melting sour solids that collect in the lower sour liquid collection zone 16 into sour liquid.
  • the heating means 30 is a heater, such as, for example, a heat exchanger or an immersion heater.
  • the apparatus 10 also includes a first level control valve assembly 32 in fluid communication with the outlet 26 in the lower sour liquid collection zone 16, and a second level control valve assembly 34 in fluid communication with the outlet 24 in the upper hydrocarbon liquid collection zone 18.
  • the first level control valve assembly 32 determines the withdrawal of sour liquid from the lower sour liquid collection zone 16 and the second level control valve assembly 34 determines the withdrawal of hydrocarbon liquid from the upper hydrocarbon liquid collection zone 18.
  • the first and second level control valve assemblies 32, 34 are operatively controlled in response to signals received from one or more probes and/or sensors disposed in the lower sour liquid collection zone 16 and/or the upper hydrocarbon liquid collection zone 18 and/or the upper vapour space 14 of the separator vessel 12, as shown in Figure 1.
  • the probes and/or sensors are arranged in use to measure one or more of physical parameters within the separator vessel selected from the group comprising differential temperature, RF capacitance, differential pressure, hydrostatic pressure, and so forth, as will be known to persons skilled in the art.
  • the probes and sensors illustrated in Figure 1 are illustrative of differential temperature changes between the lower sour liquid collection zone 16, the upper hydrocarbon liquid collection zone 18, and the upper vapour space 14 of the separator vessel 12, respectively.
  • the apparatus 10 also includes a means 36 for directing vapour generated in the sour liquid collection zone 16 to the upper vapour space 14.
  • the means 36 is configured to minimise disturbance of the interface 11 between the sour liquid and hydrocarbon liquid.
  • the means 36 comprises a riser assembly 38 having a vertical component 40 extending upwardly from a lower conical component 42, the lower conical component 42 being disposed in the sour liquid collection zone 16 and the vertical component 40 extending through the hydrocarbon liquid collection zone 18 and terminating in the upper vapour space 14 of the separator vessel 12. Hydrocarbon vapour generated in the sour liquid collection zone 16 enters the lower conical component 42 and passes upwardly through the lower conical component 42 and the vertical component 40 and exits the vertical component 40 in the upper vapour space 14.
  • the riser assembly 38 may be formed from material having low thermal conductivity. Additionally or alternatively, the riser assembly 30 is provided with nonstick surfaces and downward sloping surfaces to prevent falling solids from accumulating thereon.
  • the vertical component 40 may be configured to prevent sour solids from entering from the top.
  • the vertical component 40 is provided with a cap 44 having downwardly inclined surfaces.
  • the cap may be configured to expel hydrocarbon vapour substantially laterally into the upper vapour space.
  • the cap may also be formed from material having low thermal conductivity and/or be provided with non-stick surfaces for reasons as described above .
  • the separator vessel 12 may be also provided with an inlet (not shown) disposed in the lower sour liquid collection zone 16, wherein the inlet is configured to introduce sour liquid into the lower sour liquid collection zone 16. This particular feature may be useful to facilitate establishment of two distinct liquid layers in the separator vessel 12, particularly during start up operations.
  • the apparatus 10 ' shown in Figure 2 includes all the features described with reference to Figure 1. Additionally, the separator vessel 12 is provided with a weir 46 disposed in the lower sour liquid collection zone 16. Said weir 46 is constructed of a low thermal conductivity material to minimize heat transfer from the sour liquid to the collected hydrocarbon liquid.
  • the apparatus 10" shown in Figure 3 operates on a similar basis to the apparatuses described with reference to Figures 1 and 2 except that it is configured to separate a sweetened hydrocarbon gas and a sour liquid.
  • a liquid level 15 of the sour liquid is controlled by the first level control valve assembly 32 in fluid communication with the outlet 26 in the lower sour liquid collection zone 16.
  • the sour gas stream may be any stream of gas that comprises hydrocarbons and sour species.
  • Illustrative examples of such sour gas streams include, but are not limited to, natural gas, coal seam gas, associated gas, landfill gas, and biogas .
  • the composition of the sour gas stream may vary significantly but the sour gas stream will generally contain methane, ethane, higher hydrocarbons (C3+) , water, and sour species.
  • our species means any one or more of carbon dioxide, hydrogen sulphide, carbon disulfide, carbonyl sulphide, mercaptans (R- SH, where R is an alkyl group having one to 20 carbon atoms) , sulphur dioxide, aromatic sulphur-containing compounds, and aromatic hydrocarbons such as benzene, toluene, xylene, naphthalenes, and so forth.
  • the sour gas stream that is used in the present process has been dehydrated.
  • the sour gas stream has a water content of less than 50 ppm, and preferably less than 7 ppm for pipeline specification gas, and a water content of less than 1 ppm for LNG specification gas.
  • Any suitable process for dehydrating the sour gas stream can be used.
  • An example of a suitable dehydration process includes the adsorption of water from the gas stream with molecular sieves or silica gel.
  • dehydration by adsorption using glycol or methane may be possible, or other suitable dehydration processes known in the art.
  • the sour gas stream is cooled to a temperature below the temperature at which (hydrocarbon) liquids form and/or just above the temperature at which sour solids form prior to introducing the sour gas stream into the separator vessel 12 through valve 28.
  • the sour gas stream may be cooled by indirect heat exchange with a cooling stream or a refrigerant stream in a heat exchanger or cold box.
  • the sour gas stream may be cooled by expansion in one or more conventional gas expansion devices.
  • the sour gas stream is cooled to a temperature in a range of about -65 0 C - -70 0 C.
  • the cooled sour gas stream is further cooled to a temperature at or just below the temperature at which sour solids form by expanding the cooled sour gas stream through the Joule-Thomson valve 28 that, together with line 15, defines the inlet 20 of the separator vessel 12.
  • Other suitable expansion means such as a turbo expander to further cool the stream as it enters the separator vessel 12 may be used, including using a turbo expander in sequential combination with the Joule-Thomson valve.
  • the process of expanding the sour gas stream upon introduction to the upper vapour space 14 of the separator vessel 12 is arranged to afford temperature and pressure conditions within the upper vapour space 14 of the separator vessel 12 at which the sour species contained in the sour gas stream solidify and/or liquefy.
  • the process of expansion typically cools the gas stream entering the upper vapour space 14 of the separator vessel 12 at inlet 20 to a temperature in a range of about -80 to -95 0 C under a pressure within a pressure range of 15 to 20 bar.
  • liquid hydrocarbons, NGLs Upon cooling the sour gas stream, as described above, liquid hydrocarbons, NGLs, also form under the temperature and pressure conditions in the upper vapour space 14 of the separator vessel 12 together with methane vapour.
  • the sour liquid and/or solids and the hydrocarbon liquid so formed in the upper vapour space 14 separate from the vapour under gravity and density, thereby producing sweetened gas in the upper vapour space 14.
  • the liquids and solids then separate further under density and gravity to the lower sour liquid collection zone 16 and the upper hydrocarbon liquid collection zone 18, producing a slurry of sour solids and sour liquids in the lower sour liquid collection zone 16 and hydrocarbon liquid in the upper hydrocarbon liquid collection zone 18.
  • Droplets and/or particles of sour species continuously fall through the upper hydrocarbon liquid collection zone 18 to the lower sour liquid collection zone 16.
  • An interface 11 is formed between the hydrocarbon liquid and the sour liquid, as well as a gas-liquid interface 13 between the sweetened gas and the hydrocarbon liquid.
  • sour gas is lean in condensable hydrocarbon components only a single liquid phase of substantially sour liquid may form in the lower sour liquid collection zone 16, wherein a gas-liquid interface 15 between the sweetened gas and the sour liquid is formed.
  • the sour liquid may contain small amounts of condensable hydrocarbons which may be subsequently vapourised as the temperature of the sour liquid is raised to melt solid sour species.
  • Sweetened gas may be withdrawn from the separator vessel 12 via outlet 22.
  • the slurry of sour solids in sour liquid is then heated to a temperature at least marginally greater than the solidification temperature of the sour solids to convert the sour solids to the sour liquid in the lower sour liquid collection zone 16 of the separator vessel 12.
  • the separator vessel 12 is provided with an immersion heater 30 which heats the slurry up to a temperature marginally greater than the melting point temperature of the sour solids.
  • the immersion heater 30 comprises the heat exchanger which cools the gas stream while heating the slurry.
  • the immersion heater 30 may comprise an electric immersion heater.
  • the hydrocarbon liquid phase and the sour liquid phase are not only distinguished by density but by their respective temperatures.
  • the upper hydrocarbon liquid phase is typically at a temperature close to the temperature maintained in the upper vapour space 14 (i.e. about -80 0 C - -90 0 C) whereas the lower sour liquid phase is maintained at a temperature approximately 5 0 C above the freezing point of carbon dioxide, and is significantly warmer (i.e. typically at about -55 0 C to -60 0 C) .
  • Operation of the apparatus to maintain and establish two distinct liquid phases is advantageous in order to prevent condensable hydrocarbons mixing with and being extracted along with the sour species. Additionally, the colder hydrocarbon liquid phase effectively insulates the upper vapour space 14, leading to easier maintenance of desired temperatures, a lower residual concentration of sour species in the upper vapour space 14, and improved separation of sweetened gas and sour species. Provided the interface 11 between the hydrocarbon liquid and sour liquid can be maintained and is sufficiently spaced from the heater 30 in the lower sour liquid collection zone, entrainment of hydrocarbons in the sour liquid is minimized, and consequently reboiling of hydrocarbons is minimized, thus reducing the amount of energy input required for the system.
  • the maintenance of two liquid phases in the separator vessel 12 allows the operator to withdraw hydrocarbon liquid from the upper hydrocarbon liquid collection zone via outlet 24 and sour liquid from the lower sour liquid collection zone via outlet 26.
  • Sour liquid may be directly pumped to a sequestration site, or disposed of for retail sale.
  • the sour liquid Prior to sequestration or storage, the sour liquid may be used as a cooling stream in any one or more of the heat exchangers of the apparatus 10 to conserve energy within the apparatus 10.
  • Withdrawing the hydrocarbon liquid and/or withdrawing the sour liquid is performed in a manner to maintain a substantially stable interface between the hydrocarbon liquid and the sour liquid in the separator vessel.
  • the hydrocarbon liquid and/or the sour liquid are controllably withdrawn with respective first and second level control valve assemblies in response to signals received from one or more probes and/or sensors disposed in the lower sour liquid collection zone and/or the upper hydrocarbon liquid collection zone and/or the upper vapour space of the separator vessel for determining the interface.
  • Information from the probes and/or sensors is also used to maintain the interface 13 between the upper vapour space 14 and the hydrocarbon liquid, the depth of the hydrocarbon liquid phase so that the cooling/insulating effect between the upper vapour space 14 and the sour liquid is maintained, and the desired level of the interface 11 in the separator vessel 12.
  • the interface 11 between the hydrocarbon liquid and the sour liquid is maintained at a desired level in the separator vessel 12 so as not to approach the heating means 30 in the lower sour liquid collection zone 16 of the separator vessel 12 and trigger vapourisation of hydrocarbons in the hydrocarbon liquid.
  • the separator vessel 12 is preferably provided with the means 36 for directing this vapour to the upper vapour space 14, even more preferably the riser assembly 38 described above. Hydrocarbon vapour generated in the sour liquid collection zone 16 passes upwardly through the lower conical component 42 and the vertical component 40 and exit the vertical component 40 in the upper vapour space 14. In this way, the means 36 is configured to minimize disturbance of the interface 11 between the sour liquid and hydrocarbon liquid.
  • the apparatus of the present invention in its various embodiments, is configured to achieve effective control of the temperature of the one or more liquid phases in the separator vessel 12. The temperature of the one or more liquid phases may be controlled by adjusting the current input of an electrical heater or by using a by-pass control valve in a process heat exchanger.
  • Effective control of the temperature in the one of more liquid phases is not only required to sufficiently melt solid sour species to enable withdrawal of liquid sour species, but it is also required to prevent excessive boil off of liquid hydrocarbons which would significantly effect the upper vapour space 14 and composition of the sweetened gas in the separator vessel 12.
  • Continuous melting of solids in the sour liquids collection zone 16 is important to avoid excessive solids accumulation therein which would cause blockage of liquid drain lines. Additionally, it is preferable that there is continuous introduction and melting of solids in the sour liquid collection zone 16 at a controllable rate, and avoidance of sudden rises in liquid level, temperature disruption, and volume increase by solids which fall into the sour liquid collection zone after having accumulated on the walls of the separator vessel 12.

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Abstract

L'invention concerne un dispositif et un procédé pour séparer un gaz acide en gaz adouci et liquide acide. L'appareil comprend une cuve de séparation dotée d'un espace de vapeur et une zone de collecte de liquide acide ; un moyen pour introduire le flux de gaz acide dans l'espace de vapeur, l'espace de vapeur étant agencé de façon à fonctionner dans des conditions selon lesquelles l'introduction du courant de gaz acide dans l'espace de vapeur produit un mélange de liquide acide et/ou de solides, de vapeur d'hydrocarbures et, en option, de liquide à base d'hydrocarbures, le liquide acide et/ou les solides et le liquide à base d'hydrocarbures, le cas échéant, se séparant sous l'effet de la gravité et de la densité vers la zone de collecte de liquide acide, produisant ainsi du gaz adouci dans l'espace de vapeur ; un moyen de chauffe dans la zone de collecte de liquide acide pour faire fondre les solides acides collectés dans la zone de collecte de liquide acide et obtenir un liquide acide ; une sortie pour extraire le gaz adouci de l'espace de vapeur ; une sortie pour extraire le liquide acide de la zone de collecte de liquide acide ; et un moyen pour contrôler un niveau du liquide acide dans la cuve de séparation.
PCT/AU2010/000723 2009-06-12 2010-06-11 Dispositif et procédé pour séparer un gaz acide en gaz adouci et liquide acide Ceased WO2010141996A1 (fr)

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AU2009902743A AU2009902743A0 (en) 2009-06-12 Apparatus and process for separating a sour gas into sweetened gas and sour liquid
AU2009902743 2009-06-12

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9331938B2 (en) 2012-04-13 2016-05-03 Nicira, Inc. Extension of logical networks across layer 3 virtual private networks
WO2016075400A1 (fr) 2014-11-14 2016-05-19 Engie Procede et systeme de traitement et de separation d'un gaz non conventionnel
EP3628951A1 (fr) * 2018-09-26 2020-04-01 Hysytech S.r.l. Séparateur flash pour le traitement d'un mélange liquide contenant du méthane liquéfié et du dioxyde de carbone de gaz et installation de production de biométhane ou de gaz naturel liquéfié comprenant un tel séparateur flash

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Publication number Priority date Publication date Assignee Title
US3798918A (en) * 1971-04-15 1974-03-26 Chicago Bridge & Iron Co Method and apparatus for purifying natural gas to be liquefied and stored
US4001116A (en) * 1975-03-05 1977-01-04 Chicago Bridge & Iron Company Gravitational separation of solids from liquefied natural gas
US4187689A (en) * 1978-09-13 1980-02-12 Chicago Bridge & Iron Company Apparatus for reliquefying boil-off natural gas from a storage tank
US5819555A (en) * 1995-09-08 1998-10-13 Engdahl; Gerald Removal of carbon dioxide from a feed stream by carbon dioxide solids separation

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3798918A (en) * 1971-04-15 1974-03-26 Chicago Bridge & Iron Co Method and apparatus for purifying natural gas to be liquefied and stored
US4001116A (en) * 1975-03-05 1977-01-04 Chicago Bridge & Iron Company Gravitational separation of solids from liquefied natural gas
US4187689A (en) * 1978-09-13 1980-02-12 Chicago Bridge & Iron Company Apparatus for reliquefying boil-off natural gas from a storage tank
US5819555A (en) * 1995-09-08 1998-10-13 Engdahl; Gerald Removal of carbon dioxide from a feed stream by carbon dioxide solids separation

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9331938B2 (en) 2012-04-13 2016-05-03 Nicira, Inc. Extension of logical networks across layer 3 virtual private networks
WO2016075400A1 (fr) 2014-11-14 2016-05-19 Engie Procede et systeme de traitement et de separation d'un gaz non conventionnel
EP3628951A1 (fr) * 2018-09-26 2020-04-01 Hysytech S.r.l. Séparateur flash pour le traitement d'un mélange liquide contenant du méthane liquéfié et du dioxyde de carbone de gaz et installation de production de biométhane ou de gaz naturel liquéfié comprenant un tel séparateur flash

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