WO2010003894A1 - Procédé destiné à éliminer un contaminant gazeux d'un courant gazeux contaminé - Google Patents

Procédé destiné à éliminer un contaminant gazeux d'un courant gazeux contaminé Download PDF

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Publication number
WO2010003894A1
WO2010003894A1 PCT/EP2009/058403 EP2009058403W WO2010003894A1 WO 2010003894 A1 WO2010003894 A1 WO 2010003894A1 EP 2009058403 W EP2009058403 W EP 2009058403W WO 2010003894 A1 WO2010003894 A1 WO 2010003894A1
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WO
WIPO (PCT)
Prior art keywords
gas
liquid
gas stream
process according
vessel
Prior art date
Application number
PCT/EP2009/058403
Other languages
English (en)
Inventor
Diki Andrian
Rick Van Der Vaart
Original Assignee
Shell Internationale Research Maatschappij B.V.
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
Application filed by Shell Internationale Research Maatschappij B.V. filed Critical Shell Internationale Research Maatschappij B.V.
Priority to US13/003,547 priority Critical patent/US20110154856A1/en
Priority to EP09793930A priority patent/EP2307530A1/fr
Priority to EA201100181A priority patent/EA201100181A1/ru
Priority to CA2730637A priority patent/CA2730637A1/fr
Priority to CN2009801264907A priority patent/CN102089411A/zh
Publication of WO2010003894A1 publication Critical patent/WO2010003894A1/fr

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Classifications

    • 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, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
    • B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
    • B01D45/16—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces generated by the winding course of the gas stream, the centrifugal forces being generated solely or partly by mechanical means, e.g. fixed swirl vanes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • B01D46/0027—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with additional separating or treating functions
    • B01D46/003—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with additional separating or treating functions including coalescing means for the separation of liquid
    • B01D46/0031—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with additional separating or treating functions including coalescing means for the separation of liquid with collecting, draining means
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
    • B01D50/20—Combinations of devices covered by groups B01D45/00 and B01D46/00
    • 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, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • 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
    • F25J3/0605—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
    • 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
    • F25J3/067—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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/10—Processes or apparatus using other separation and/or other processing means using combined expansion and separation, e.g. in a vortex tube, "Ranque tube" or a "cyclonic fluid separator", i.e. combination of an isentropic nozzle and a cyclonic separator; Centrifugal separation
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • 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

Definitions

  • the invention relates to a process for removing one or more gaseous contaminants, such as carbon dioxide or hydrogen sulphide, from a contaminated gas stream containing methane, especially a natural gas stream.
  • the invention further relates to a device for carrying out the process and to the purified gas stream obtainable by the process.
  • WO 2004/070297 a process for removing gaseous contaminants from a natural gas stream is described.
  • water is removed from the feed gas stream by cooling, the cooling resulting in methane hydrate formation.
  • This step is followed by separation of the hydrates and further cooling of the remaining gas stream, resulting in the formation of solid acidic contaminants.
  • a cleaned natural gas stream is obtained. Heating is used to convert the solid contaminants into a slurry or liquid.
  • the slurry or liquid is removed from the separation zone.
  • special measures are necessary to remove also the smallest solid particles from the gas stream.
  • WO 2003/062725 a process is described for the removal of freezable species from a natural gas stream by cooling a natural gas stream to form a slurry of solid acidic contaminants in compressed liquefied natural gas.
  • the solids are separated from the liquid by means of a cyclone. It will be clear that a complete separation of the liquid from the solids is not easily achieved.
  • WO 2007/030888 a process is described similar to the process described in WO 2004/070297, followed by washing the cleaned natural gas stream with methanol.
  • the process according to the present invention comprises no more than two steps requiring relatively simple equipment only. In the first step the contaminated gas stream containing methane is cooled until liquid contaminants condense, followed by a simple gas/liquid separator, not needing any rotating equipment and not needing any energy for a distillation section.
  • the process provides a process for removing one or more gaseous contaminants from a contaminated feed gas stream, the process comprising 1) providing the contaminated feed gas stream, 2) cooling the contaminated feed gas stream to a temperature at which liquid contaminant is formed as well as a contaminant depleted gaseous phase, and 3) separating the two phases by introducing them into a gas/liquid separator vessel, comprising a gas/liquid inlet at an intermediate level, a liquid outlet arranged below the gas/liquid inlet and a gas outlet arranged above the gas/liquid inlet, in which vessel a normally horizontal coalescer is present above the gas/liquid inlet and over the whole cross-section of the vessel and in which vessel a centrifugal liquid separator is arranged above the coalescer and over the whole cross-section of the vessel, the liquid separator comprising one or more swirl tubes.
  • the process is a rather easy and uncomplicated process. It actually comprises only a cooling step, followed by a simple gas/liquid separation step, the separation step not involving any moving equipment and not comprising any energy consuming steps.
  • a vertical gas/liquid separator vessel the process can be performed in a device only needing a relatively small plot space.
  • the gas/liquid inlet comprises an admittance with a supply and distribution assembly extending horizontally in the separator vessel.
  • the inlet is a simple pipe, having a closed end and a number of perforations evenly distributed over the length of the pipe.
  • the pipe may have a tapered or conical shape.
  • One or more cross pipes may be present to create a grid system to distribute the gas-liquid mixture more evenly over the cross-section of the vessel.
  • the assembly includes a chamber, e.g. a longitudinal box- like structure, connected to the gas inlet and having at least one open vertical side with a grid of guide vanes disposed one behind each other, seen in the direction of the flow.
  • the gas is evenly distributed by the guide vanes over the cross-section of the column, which brings about an additional improvement of the liquid separation in the coalescer/centrifugal separator combination.
  • a further advantage is that the supply and distribution assembly separates from the gas any waves of liquid which may suddenly occur in the gas stream, the separation being effected by the liquid colliding with the guide vanes and falling down inside the column.
  • the box structure narrows down in the direction of the flow. After having been distributed by the vanes over the column cross-section, the gas flows up to the coalescer.
  • the longitudinal chamber has two open vertical sides with a grid of guide vanes. Suitable gas/liquid inlets are described in e.g.
  • a suitable, commercially available gas/liquid inlet is a Schoepentoeter inlet device.
  • coalescers There are numerous horizontal coalescers available, especially for vertical columns.
  • a well-known example of a coalescer is a wire mesh. All of these are relatively tenuous (large permeability) and have a relatively large specific (internal) plot space. Their operation is based on drop capture by collision of drops with internal surfaces, followed by drop growth on these surfaces, and finally by removal of the grown drop either by the gas or by gravity.
  • the horizontal coalescer can have many forms which are known per se and may, for example, consist of a bed of layers of gauze, especially metal or non-metal gauze, e.g. organic polymer gauze, or a layer of vanes or a layer of structured packing. Also unstructured packings can be used and also one or more trays may be present. All these sorts of coalescers have the advantage of being commercially available and operating efficiently in the column according to the invention. See also Perry's Chemical Engineers' Handbook, Sixth edition, especially Chapter 18. See also EP 195464.
  • the centrifugal liquid separator in one of its most simple forms may comprise a horizontal plate and one or more vertical swirl tubes extending downwardly from the plate, each swirl tube having one or more liquid outlets below the horizontal plate at the upper end of the swirl tube.
  • the centrifugal liquid separator comprises one or more vertical swirl tubes extending upwardly from the plate, each swirl tube having one or more liquid outlets at the upper end.
  • the plate is provided with a downcomer, preferably a downcomer that extends to the lower end of the separator vessel.
  • the centrifugal liquid separator comprises two horizontal trays between which vertical open-ended swirl tubes extend, each from an opening in the lower tray to some distance below a coaxial opening in the upper tray, means for the discharge of secondary gas and of liquid from the space between the trays outside the swirl tubes, and means provided in the lower part of the swirl tubes to impart to the gas/liquid a rotary movement around the vertical axis .
  • the liquid separator is also preferably provided with vertical tube pieces which project down from the coaxial openings in the upper tray into the swirl tubes and have a smaller diameter than these latter. This arrangement enhances the separation between primary gas on the one hand and secondary gas and liquid on the other hand, since these latter cannot get from the swirl tubes into the openings in the upper tray for primary gas .
  • the means for discharging the secondary gas from the space between the trays consist of vertical tubelets through the upper tray, and the means for discharging liquid from the space between the trays consist of one or more vertical discharge pipes which extend from this space to the bottom of the column.
  • This arrangement has the advantage that the secondary gas, after having been separated from liquid in the said space between the trays, is immediately returned to the primary gas, and the liquid is added to the liquid at the bottom of the column after coming from the coalescer, so that the secondary gas and the liquid removed in the centrifugal separator do not require separate treatment.
  • openings are preferably provided in accordance with the invention at the top of the swirl tubes for discharging liquid to the space between the trays outside the swirl tubes. This has the advantage that less secondary gas is carried to the space between the trays.
  • a suitable, commercially available centrifugal separator is a Shell Swirltube deck.
  • the separation vessel comprises a second normally horizontal liquid coalescer above the centrifugal liquid separator and over the whole cross-section of the vessel.
  • the second coalescer is arranged to remove liquids from the secondary gas.
  • the second coalescer is a bed of one or more layers of gauze, especially metal or non-metal gauze, e.g. organic polymer gauze.
  • the second normally horizontal liquid coalescer is situated above the secondary gas outlets, for instance in the way as described in EP 83811, especially as depicted in Figure 4.
  • the contaminated gas stream may be any gas stream containing acidic contaminants.
  • the contaminated gas stream is a methane containing gas stream, for instance from natural sources as natural gas, associated gas or coal bed methane or from industrial sources as refinery streams or synthetic sources as Fischer-Tropsch streams or from biological sources as anaerobic waste or manure fermentation.
  • the amount of methane present may vary over a wide range, e.g. from 3 to 90 vol%, preferably 5 and 80 vol% methane, more preferably between 10 and 75 vol%.
  • the contaminated gas stream may also be a syngas stream comprising carbon dioxide, a flue gas stream or a gas stream obtained after combustion of coal.
  • Syngas is a mixture of carbon monoxide and hydrogen.
  • a syngas stream comprising carbon dioxide is generally obtained after converting part or most of the carbon monoxide to carbon dioxide in a so-called water gas shift reaction.
  • the acidic contaminants in the feedstream are especially carbon dioxide and hydrogen sulphide, although also carbonyl sulphide (COS), carbon disulphide (CS2), mercaptans, sulphides and aromatic sulphur compounds may be present.
  • Beside acidic contaminants, also inerts may be present, for instance nitrogen and noble gases as argon and helium.
  • the amount of acidic contaminants present in the feed gas may vary over a wide range.
  • the amount of carbon dioxide in the feed gas is suitably between 15 and 90 vol%, preferably between 20 and 75 vol%.
  • the amount of hydrogen sulphide in the feed gas is suitably between 5 and 55 vol%, preferably between 10 and 45 vol%.
  • the cooling of the feed gas may be done by methods known in the art. For instance, cooling may be done against an external cooling fluid. In the case that the pressure of the feed gas is sufficiently high, cooling may be obtained by expansion of the feed gas stream. Combinations may also be possible.
  • a suitable method to cool the feed gas stream is done by nearly isentropic expansion, especially by means of an expander, preferably a turbo expander or laval nozzle.
  • Another suitable method is to cool the feed gas stream by isenthalpic expansion, preferably isenthalpic expansion over an orifice or a valve, especially over one or more Joule-Thomson valves.
  • more than one expander is used, as this enables influencing the droplet size and/or droplet size distribution .
  • the feed gas stream is pre-cooled before expansion. This may be done against an external cooling loop or against a cold process stream, e.g. liquid acidic contaminant.
  • the gas stream is pre-cooled before expansion to a temperature between 15 and -35 0 C, preferably between -10 0 C and -20 0 C.
  • Pre- cooling may be done against internal process streams. Especially when the feed gas stream has been compressed, the temperature of the feed gas stream may be between 100 and 150 0 C. In that case air cooling may be used to decrease the temperature first, optionally followed by further cooling.
  • Another suitable cooling method is heat exchange against a cold fluidum, especially an external refrigerant, e.g. a propane cycle, an ethane/propane cascade or a mixed refrigerant cycle, optionally in combination with an internal process loop, suitably a carbon dioxide stream (liquid or slurry) , a cold contaminant depleted stream or washing fluid or in which the cooling is done by compression, cooling and expansion .
  • an external refrigerant e.g. a propane cycle, an ethane/propane cascade or a mixed refrigerant cycle
  • an internal process loop suitably a carbon dioxide stream (liquid or slurry) , a cold contaminant depleted stream or washing fluid or in which the cooling is done by compression, cooling and expansion .
  • the feed gas stream is cooled to a temperature between -30 and -80 0 C, especially between -40 and -60 0 C. At these temperatures liquids will be formed.
  • the raw feed gas stream may be pre-treated to partially or completely remove of water and optionally some heavy hydrocarbons. This can for instance be done by means of a pre-cooling cycle, against an external cooling loop or a cold internal process stream. Water may also be removed by means of pre-treatment with molecular sieves, e.g. zeolites, or silica gel or alumina oxide or other drying agents. Water may also be removed by means of washing with glycol, MEG, DEG or TEG, or glycerol. The amount of water in the gas feed stream is suitably less than 1 vol%, preferably less than 0.1 vol%, more preferably less than 0.01 vol%.
  • the feedstream for the process of the invention will suitably have a pressure between 10 and 120 bara, or even up till 160 bara. Especially, the feedstream has a pressure between 15 and 70 bara, preferably between 20 and 50 bara.
  • the feedstream, preferably pretreated suitably has a temperature between -30 and 150 0 C, suitably between -20 and 70 0 C, preferably between 0 and 50 0 C.
  • the contaminant depleted gaseous phase is further purified, e.g. by extraction of remaining acidic components with a chemical solvent, e.g. an aqueous amine solution, especially aqueous ethanolamines, such as DIPA, DMA, MDEA, etc., or with a physical solvent, e.g. cold methanol, DEPG, NMP, etc.
  • a chemical solvent e.g. an aqueous amine solution, especially aqueous ethanolamines, such as DIPA, DMA, MDEA, etc.
  • a physical solvent e.g. cold methanol, DEPG, NMP, etc.
  • the contaminated gas stream is continuously provided, continuously cooled and continuously separated.
  • FIG. 1 a device is shown for carrying out the process of the present invention.
  • a dry feed stream (water content 20 ppm, 60 bara) flows via pipe 1 to turbo-expander 2. In the expander the temperature drops to -45 0 C.
  • the feed gas comprises 40 vol% of carbon dioxide, 2 vol% of ethane and 58 vol% of methane.
  • the resulting gas/liquid mixture is introduced into vertical gas/liquid separator 3 via supply and distribution assembly 4. Most of the liquid will flow down to the lower end of the separator and leave the separator via liquid outlet 5.
  • the gaseous stream comprising larger and smaller droplets will flow upwards via liquid coalescer 6, centrifugal separator 7 and a second liquid coalescer 8 to the top of the separator vessel, and leave the separator vessel via gas outlet 9.

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

Abstract

La présente invention concerne un procédé destiné à éliminer un ou plusieurs contaminants gazeux d'un courant gazeux d'alimentation contaminé, le procédé comprenant les étapes consistant à 1) fournir le courant gazeux d'alimentation contaminé, 2) refroidir le courant gazeux d'alimentation contaminé jusqu'à une température à laquelle le contaminant liquide se forme ainsi qu'une phase gazeuse appauvrie en contaminant, et 3) séparer les deux phases en les introduisant dans une cuve de séparation gaz/liquide, comprenant une entrée de gaz/liquide à un niveau intermédiaire, une sortie de liquide située en dessous de l'entrée de gaz/liquide et une sortie de gaz située au dessus de l'entrée de gaz/liquide. Dans cette cuve, un coalesceur normalement horizontal est présent au-dessus de l'entrée de gaz / liquide et par‑dessus l'ensemble de la section transversale de la cuve, et un séparateur de liquides par centrifugation est disposé au-dessus du coalesceur et par-dessus l'ensemble de la section transversale de la cuve, le séparateur de liquides comprenant un ou plusieurs tubes de tourbillonnement. Le courant gazeux contaminé peut être un courant gazeux contenant du méthane, en particulier un courant de gaz naturel, ou un courant gazeux provenant d'un procédé de gazéification ou de combustion. L'invention concerne en outre un dispositif destiné à effectuer le procédé ainsi qu'à obtenir le courant gazeux purifié.
PCT/EP2009/058403 2008-07-10 2009-07-03 Procédé destiné à éliminer un contaminant gazeux d'un courant gazeux contaminé WO2010003894A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
US13/003,547 US20110154856A1 (en) 2008-07-10 2009-07-03 Process for removing a gaseous contaminant from a contaminated gas stream
EP09793930A EP2307530A1 (fr) 2008-07-10 2009-07-03 Procédé destiné à éliminer un contaminant gazeux d'un courant gazeux contaminé
EA201100181A EA201100181A1 (ru) 2008-07-10 2009-07-03 Способ удаления газообразного загрязнителя из потока загрязнённого газа
CA2730637A CA2730637A1 (fr) 2008-07-10 2009-07-03 Procede destine a eliminer un contaminant gazeux d'un courant gazeux contamine
CN2009801264907A CN102089411A (zh) 2008-07-10 2009-07-03 从污染的气体物流中脱除气态污染物的方法

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP08160067 2008-07-10
EP08160067.8 2008-07-10

Publications (1)

Publication Number Publication Date
WO2010003894A1 true WO2010003894A1 (fr) 2010-01-14

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PCT/EP2009/058403 WO2010003894A1 (fr) 2008-07-10 2009-07-03 Procédé destiné à éliminer un contaminant gazeux d'un courant gazeux contaminé

Country Status (6)

Country Link
US (1) US20110154856A1 (fr)
EP (1) EP2307530A1 (fr)
CN (1) CN102089411A (fr)
CA (1) CA2730637A1 (fr)
EA (1) EA201100181A1 (fr)
WO (1) WO2010003894A1 (fr)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8312738B2 (en) 2007-01-19 2012-11-20 Exxonmobil Upstream Research Company Integrated controlled freeze zone (CFZ) tower and dividing wall (DWC) for enhanced hydrocarbon recovery
US9149761B2 (en) 2010-01-22 2015-10-06 Exxonmobil Upstream Research Company Removal of acid gases from a gas stream, with CO2 capture and sequestration
US9423174B2 (en) 2009-04-20 2016-08-23 Exxonmobil Upstream Research Company Cryogenic system for removing acid gases from a hydrocarbon gas stream, and method of removing acid gases
CN106244272A (zh) * 2016-08-23 2016-12-21 成都正升能源技术开发有限公司 重力沉降式气液分离装置
CN106318501A (zh) * 2016-08-23 2017-01-11 成都正升能源技术开发有限公司 重力沉降式气液分离方法
US9829246B2 (en) 2010-07-30 2017-11-28 Exxonmobil Upstream Research Company Cryogenic systems for removing acid gases from a hydrocarbon gas stream using co-current separation devices
US10222121B2 (en) 2009-09-09 2019-03-05 Exxonmobil Upstream Research Company Cryogenic system for removing acid gases from a hydrocarbon gas stream
US10408534B2 (en) 2010-02-03 2019-09-10 Exxonmobil Upstream Research Company Systems and methods for using cold liquid to remove solidifiable gas components from process gas streams

Families Citing this family (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2748291A4 (fr) * 2011-11-15 2015-08-19 Shell Int Research Procédé de traitement de courants d'alimentation contenant du sulfure d'hydrogène
AU2013235610B2 (en) 2012-03-21 2015-11-19 Exxonmobil Upstream Research Company Separating carbon dioxide and ethane from a mixed stream
CA2924695C (fr) 2013-12-06 2018-10-02 Exxonmobil Upstream Research Company Procede et systeme permettant de separer un courant d'alimentation avec un mecanisme de distribution de courant d'alimentation
US9823016B2 (en) 2013-12-06 2017-11-21 Exxonmobil Upstream Research Company Method and system of modifying a liquid level during start-up operations
US9562719B2 (en) 2013-12-06 2017-02-07 Exxonmobil Upstream Research Company Method of removing solids by modifying a liquid level in a distillation tower
CA2925404C (fr) 2013-12-06 2018-02-06 Exxonmobil Upstream Research Company Procede et systeme de deshydratation d'un flux d'alimentation traite dans une tour de distillation
WO2015084495A2 (fr) 2013-12-06 2015-06-11 Exxonmobil Upstream Research Company Procédé et système de maintien d'un niveau de liquide dans une tour de distillation
CA2924402C (fr) 2013-12-06 2017-11-21 Exxonmobil Upstream Research Company Procede et dispositif pour la separation d'un flux d'alimentation au moyen de detecteurs de rayonnement
US9869511B2 (en) 2013-12-06 2018-01-16 Exxonmobil Upstream Research Company Method and device for separating hydrocarbons and contaminants with a spray assembly
US9874395B2 (en) 2013-12-06 2018-01-23 Exxonmobil Upstream Research Company Method and system for preventing accumulation of solids in a distillation tower
CN105723171B (zh) 2013-12-06 2018-06-05 埃克森美孚上游研究公司 采用加热设施使固体粘合不稳定和/或防止固体粘合的分离烃和污染物的方法和装置
US10393302B2 (en) 2014-06-18 2019-08-27 United Technologies Corporation Double wall tube bolted flange fitting
US10054057B2 (en) 2014-06-18 2018-08-21 United Technologies Corporation Double walled tube drainage system
CA2972796C (fr) 2015-02-27 2019-08-13 Exxonmobil Upstream Research Company Reduction d'une charge de refrigeration et de deshydratation pour un flux d'alimentation entrant dans un processus de distillation cryogenique
KR101992109B1 (ko) * 2015-03-13 2019-06-25 엑손모빌 업스트림 리서치 캄파니 병류 접촉기용 코어레서
CA2994812C (fr) 2015-09-18 2020-03-10 Exxonmobil Upstream Research Company Composant de chauffage pour reduction de la solidification dans un systeme de distillation cryogenique
WO2017052922A2 (fr) 2015-09-24 2017-03-30 Exxonmobil Upstream Research Company Usine de traitement pour hydrocarbure gazeux présentant des niveaux de contaminants variables
US10330363B2 (en) 2016-02-08 2019-06-25 Trane International Inc. Lubricant separator for a heating, ventilation, and air conditioning system
WO2017172321A1 (fr) 2016-03-30 2017-10-05 Exxonmobil Upstream Research Company Fluide de réservoir auto-sourcé pour la récupération assistée de pétrole
US10253267B2 (en) * 2016-04-06 2019-04-09 Purscrub Llc Separator that removes free liquid and particles from a gas stream
EP3720588B1 (fr) * 2017-12-06 2023-08-30 Cummins Filtration IP, Inc. Systèmes de ventilation de carter ayant un brise-turbulence pour réduire la chute de pression dans des fluides sortants tangentiellement
US11306267B2 (en) 2018-06-29 2022-04-19 Exxonmobil Upstream Research Company Hybrid tray for introducing a low CO2 feed stream into a distillation tower
WO2020005553A1 (fr) 2018-06-29 2020-01-02 Exxonmobil Upstream Research Company (Emhc-N1.4A.607) Mélange et intégration de chaleur de liquides de plateau de fusion dans une tour de distillation cryogénique
WO2020035139A1 (fr) * 2018-08-15 2020-02-20 Thyssenkrupp Industrial Solutions (Australia) Pty. Ltd. Dispositif à tube tourbillonnant en ligne pour la coalescence de gouttelettes liquides dans une application de gaz pauvre

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2792075A (en) * 1954-06-22 1957-05-14 Thermix Corp Apparatus for separating suspended mist particles from gases
US4767424A (en) * 1985-03-05 1988-08-30 Shell Oil Company Column for removing liquid from a gas
WO2005061978A1 (fr) * 2003-12-22 2005-07-07 Bp Exploration Operating Company Limited Procede de production d'un gaz naturel liquefie appauvri en azote

Family Cites Families (26)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4533372A (en) * 1983-12-23 1985-08-06 Exxon Production Research Co. Method and apparatus for separating carbon dioxide and other acid gases from methane by the use of distillation and a controlled freezing zone
US6581092B1 (en) * 1999-09-29 2003-06-17 Ricoh Co., Ltd. Method and system for remote diagnostic, control and information collection based on various communication modes for sending messages to users
US5948058A (en) * 1995-10-30 1999-09-07 Nec Corporation Method and apparatus for cataloging and displaying e-mail using a classification rule preparing means and providing cataloging a piece of e-mail into multiple categories or classification types based on e-mail object information
US6330589B1 (en) * 1998-05-26 2001-12-11 Microsoft Corporation System and method for using a client database to manage conversation threads generated from email or news messages
US6442592B1 (en) * 1998-12-11 2002-08-27 Micro Computer Systems, Inc. Message center system
US6537458B1 (en) * 1999-03-05 2003-03-25 Shell Oil Company Three-phase separator
US6496853B1 (en) * 1999-07-12 2002-12-17 Micron Technology, Inc. Method and system for managing related electronic messages
US6631398B1 (en) * 1999-07-12 2003-10-07 Micron Technology, Inc. Managing redundant electronic messages
US6701346B1 (en) * 1999-07-12 2004-03-02 Micron Technology, Inc. Managing redundant electronic messages
US6525747B1 (en) * 1999-08-02 2003-02-25 Amazon.Com, Inc. Method and system for conducting a discussion relating to an item
US6704772B1 (en) * 1999-09-20 2004-03-09 Microsoft Corporation Thread based email
WO2001051161A1 (fr) * 2000-01-07 2001-07-19 Akzo Nobel N.V. Procede et appareil d'extraction liquide-liquide
US6386520B2 (en) * 2000-02-16 2002-05-14 Shell Oil Company Fluid inlet device
US6700591B1 (en) * 2000-05-04 2004-03-02 Microsoft Corporation Variable visual indicators based on predetermined characteristics
US6807566B1 (en) * 2000-08-16 2004-10-19 International Business Machines Corporation Method, article of manufacture and apparatus for processing an electronic message on an electronic message board
US6832244B1 (en) * 2000-09-21 2004-12-14 International Business Machines Corporation Graphical e-mail content analyser and prioritizer including hierarchical email classification system in an email
FR2814378B1 (fr) * 2000-09-26 2002-10-31 Inst Francais Du Petrole Procede de pretraitement d'un gaz naturel contenant des gaz acides
US7243125B2 (en) * 2000-12-08 2007-07-10 Xerox Corporation Method and apparatus for presenting e-mail threads as semi-connected text by removing redundant material
US7003724B2 (en) * 2000-12-08 2006-02-21 Xerox Corporation Method and system for display of electronic mail
US6745197B2 (en) * 2001-03-19 2004-06-01 Preston Gates Ellis Llp System and method for efficiently processing messages stored in multiple message stores
US7359936B2 (en) * 2001-11-27 2008-04-15 International Business Machines Corporation Method and apparatus for electronic mail interaction with grouped message types
US20030163537A1 (en) * 2001-11-27 2003-08-28 International Business Machines Corporation Method and apparatus for handling conversation threads and message groupings as a single entity
US6942720B2 (en) * 2002-02-21 2005-09-13 Shell Oil Company Apparatus and method for treating a fluid
US20040044735A1 (en) * 2002-08-30 2004-03-04 International Business Machines Corporation Method and system for organizing an email thread
US7421690B2 (en) * 2003-06-23 2008-09-02 Apple Inc. Threaded presentation of electronic mail
WO2007030888A1 (fr) * 2005-09-15 2007-03-22 Cool Energy Limited Procédé et appareil destinés à la suppression d’espèces acides à partir d’un flux de gaz naturel

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2792075A (en) * 1954-06-22 1957-05-14 Thermix Corp Apparatus for separating suspended mist particles from gases
US4767424A (en) * 1985-03-05 1988-08-30 Shell Oil Company Column for removing liquid from a gas
WO2005061978A1 (fr) * 2003-12-22 2005-07-07 Bp Exploration Operating Company Limited Procede de production d'un gaz naturel liquefie appauvri en azote

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP2307530A1 *

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8312738B2 (en) 2007-01-19 2012-11-20 Exxonmobil Upstream Research Company Integrated controlled freeze zone (CFZ) tower and dividing wall (DWC) for enhanced hydrocarbon recovery
US9423174B2 (en) 2009-04-20 2016-08-23 Exxonmobil Upstream Research Company Cryogenic system for removing acid gases from a hydrocarbon gas stream, and method of removing acid gases
US10222121B2 (en) 2009-09-09 2019-03-05 Exxonmobil Upstream Research Company Cryogenic system for removing acid gases from a hydrocarbon gas stream
US9149761B2 (en) 2010-01-22 2015-10-06 Exxonmobil Upstream Research Company Removal of acid gases from a gas stream, with CO2 capture and sequestration
US10408534B2 (en) 2010-02-03 2019-09-10 Exxonmobil Upstream Research Company Systems and methods for using cold liquid to remove solidifiable gas components from process gas streams
US9829246B2 (en) 2010-07-30 2017-11-28 Exxonmobil Upstream Research Company Cryogenic systems for removing acid gases from a hydrocarbon gas stream using co-current separation devices
CN106244272A (zh) * 2016-08-23 2016-12-21 成都正升能源技术开发有限公司 重力沉降式气液分离装置
CN106318501A (zh) * 2016-08-23 2017-01-11 成都正升能源技术开发有限公司 重力沉降式气液分离方法

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EA201100181A1 (ru) 2011-06-30
CN102089411A (zh) 2011-06-08

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