WO2020035139A1 - Dispositif à tube tourbillonnant en ligne pour la coalescence de gouttelettes liquides dans une application de gaz pauvre - Google Patents

Dispositif à tube tourbillonnant en ligne pour la coalescence de gouttelettes liquides dans une application de gaz pauvre Download PDF

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Publication number
WO2020035139A1
WO2020035139A1 PCT/EP2018/072157 EP2018072157W WO2020035139A1 WO 2020035139 A1 WO2020035139 A1 WO 2020035139A1 EP 2018072157 W EP2018072157 W EP 2018072157W WO 2020035139 A1 WO2020035139 A1 WO 2020035139A1
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WO
WIPO (PCT)
Prior art keywords
gas
degrees
swirl tube
inner hub
liquid
Prior art date
Application number
PCT/EP2018/072157
Other languages
English (en)
Inventor
Karan BAGGA
Original Assignee
Thyssenkrupp Industrial Solutions (Australia) Pty. Ltd.
Thyssenkrupp Ag
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 Thyssenkrupp Industrial Solutions (Australia) Pty. Ltd., Thyssenkrupp Ag filed Critical Thyssenkrupp Industrial Solutions (Australia) Pty. Ltd.
Priority to PCT/EP2018/072157 priority Critical patent/WO2020035139A1/fr
Publication of WO2020035139A1 publication Critical patent/WO2020035139A1/fr

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Classifications

    • 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

Definitions

  • the invention relates to a gas processing arrangement for natural gas gathering and conditioning, a process for increasing the liquid droplet size in a gas stream and subsequent liquid removal from a gas stream and the use of the inventive gas processing arrangement for the improvement of the removal efficiency of fine liquid droplets ( ⁇ 5 pm) in gas streams.
  • Natural gas is still one of the most important energy sources worldwide. Especially in comparison to coal, natural gas has a significant lower C0 2 and air pollutant output. Rising concerns in regard to greenhouses gases have led to a further demand of reliable energy sources. This demand can only be partially satisfied with renewable energy sources, however the still growing energy demand and energy consumption still requires the use of conventional energy sources. In addition, recent advances in shale gas fracking have further increased the availability of shale gas.
  • Natural gas is commonly accompanied by further liquids, solids and gases.
  • the liquids comprise water and different hydrocarbons. Especially heavier hydrocarbons and water needs to be removed prior to end use in domestic and industrial applications. This process of removing water and heavier hydrocarbons is called dewpoint conditioning.
  • One common method for liquid gas separation is cryogenic cooling to achieve liquid condensation followed by cyclonic separation in a suitable tube or similar device.
  • the well-known liquid gas separation is achieved by creating a cyclic vortex stream in the gas/liquid stream of a tube. This vortex induces a centrifugal force which results in outward force directed to the tube walls.
  • the vortex can be realized by placing a swirl body inside the tube/pipe body. This swirl body can be accompanied by optional or additional air nozzles.
  • the liquid droplets are enriched near inner pipe walls. This leads to a collision of the liquid droplets with the pipe wall or with other neighboring droplets. Simultaneously, the droplet collision leads to an increased droplet size. Thereby the locally concentrated and grown droplets can be separated from the gas stream.
  • US 5,743,926 A discloses an apparatus for separation of liquid and vapor in distillation and flashing processes. Thereby a portion of the feed line to a distilling column/flasher is used as a flow-through cyclone to separate vapor and liquid components of the feed. The vortex flow is created in the flasher feed line with a swirl vane assembly having drainage slots in the bottommost portion thereof.
  • DE 1 043 285 B discloses a tubular device for separating liquids from gaseous streams.
  • the inner hub comprises four vanes with a vane angle or pitch of 180 degrees.
  • US 3,258,895 A discloses a device for separating solids from a gaseous medium.
  • WO 01/66225 A2 discloses a vapor/liquid separator comprising a hub located within a vessel below the inlet wherein the hub supports a plurality of vane elements for centrifuging a mixture as the mixture proceeds through the vessel.
  • the device further describes a vapor outlet and an outlet for withdrawing the liquid phase.
  • WO 99/03554 A1 discloses a swirl tube for a vapor liquid contact tray.
  • the invention relates to the use of a venturi swirl tube to maximize the mass and/or energy transfer in a vapor liquid process column.
  • the object of the present invention is also solved by a process for increasing the liquid droplet size in a gas stream according to claim 13. Preferred embodiments of the process are subject to the corresponding dependent claims.
  • the object of the present invention is further solved by the use of the inventive gas processing arrangement for the improvement of removal efficiency of fine liquid droplets in gas streams, preferably natural gas or synthesis gas.
  • the gas processing arrangement for natural gas gathering and conditioning at least comprises a gas source and a horizontally placed swirl tube arrangement connected upstream with the gas source.
  • the swirl tube arrangement comprises an outer pipe (or outer tube), an inner hub (or inner tube/pipe) fixed within the outer pipe and four or more vanes attached to the inner hub.
  • the term“gas source” refers to a device which is able to provide, store or transport a gas. This may include natural or artificial gas reservoirs, tanks, gasholder and/or underground gas reservoirs.
  • the term“pipe” is interchangeable with the term“tube”.
  • the term“hub” is interchangeable with the term“tube” or“pipe”.
  • connection means which are able/suitable to transport or transfer process gases and liquids (or mixtures thereof), e.g. pipes, ducts, pumps, compressors, hoses and further includes tanks and/or similar adjustable storage devices.
  • the gas processing arrangement for natural gas gathering and conditioning at least comprises a gas source and a horizontally placed swirl tube arrangement connected upstream with the gas source.
  • the swirl tube arrangement comprises an outer pipe, an inner hub fixed within the outer pipe and four or more vanes.
  • the inner hub is closed (fitted with aerodynamic heads) on both sides.
  • the vanes are attached to the inner hub along a fixing line comprising a curved line and a straight line and wherein the curved line forms at least 20 % of the fixing line.
  • the term“attached to the inner hub along a fixing line” describes the geometric arrangement and fixation of the vanes on the inner hub.
  • the term“fixing line” does not refer to specific device feature but refers to the attachment form/geometry of the vanes on the inner hub (alongside a“virtual” line).
  • the vanes comprise at least two sections.
  • the first section of the vane comprises a contact area with the inner hube, which is characterized in that the contact area can be defined by straight lines.
  • This section is defined as a fixing line comprising a straight line.
  • the second section of the vane comprises a contact area with the inner hub, which is characterized in that the contact area can be defined by curved lines.
  • the curved line forms at least 30 %, more preferably 40 % to 60 % of the fixing line.
  • the curved line is oriented at the front end (in the direction of flow) of the fixing line. Therefore, a gas stream passes at first through a first vane part with a curved basic geometry and afterwards a second vane part with a linear basic geometry.
  • basic geometry refers to the contact surface between the vane and the inner hub alongside the fixing line.
  • the vane angle a [alfa] of the straight line (as a part of the above described fixing line referring to the vane contact area with the inner hub) is in the range of (including) 20° [degrees] to 70° [degrees], more preferably in the range between (including) 40° [degrees] to 60° [degrees].
  • the term“vane angle” refers to the angle between a (virtual) line through the inner hub, located orthogonal to the inner central axis in the direction of flow and located and connected with the end point of the straight line.
  • the end point of the straight line refers to the end point of the respective vane, too.
  • the vane angle is further defined in figure 2.
  • the specific vane angle range supports and increases the coalescence of the liquid droplets in the gas stream within the outer pipe. The vane angle is measured in an unfolded view as described in figure 2.
  • the vane overlap b [beta] of the straight line (as a part of the above described fixing line referring to the vane contact area with the inner hub) is in the range of 10° [degrees] to 40° [degrees], more preferably 20° [degrees] to 30 [degrees].
  • the vane overlap is measured as the smaller angle of a parallelogram formed by two adjacent straight lines.
  • the vane overlap angle is measured in an unfolded view as described in figure 2.
  • the inner hub is closed, more preferably closed via two aerodynamically profiled endcaps.
  • the vanes are connected with an inner wall of the outer pipe.
  • the reduction of free space between the vanes and angle b [beta] and the inner wall of the outer pipe increases the vortex forming and centrifugal force within the outer pipe.
  • the ratio between the diameter of the outer pipe and the diameter of the inner hub is in the range of 1.5 to 4, more preferably in the range of 2 to 3.
  • a gas expanding unit is arranged between the gas source and the swirl tube arrangement. More preferably, the gas expanding unit comprises a Joule-Thompson valve which generates liquid droplets due to cooling. In high gas volume fraction gas, the liquid droplets generated may be otherwise too fine and droplet size distribution is often unpredictable and influenced by piping geometry.
  • the swirl tube arrangement is connected (downstream) with a liquid/gas separator. The swirl tube arrangement enables a liquid droplet grow based on droplet coalescence as described above. These grown droplets can be easily removed in the downstream liquid/gas separator. Contrary to a setup without the swirl tube arrangement according to the invention, the liquid droplets can be removed from a very dry gas stream. e.g. below 0.5 wt.
  • the swirl tube arrangement is connected (upstream) with the gas expanding unit and connected (downstream) with the gas/liquid separator.
  • This setup allows generation of liquid in the gas expanding unit, a droplet grow via coalescence in the swirl tube arrangement and a final liquid droplet removal in the gas/liquid separator.
  • the complete setup comprises in the direction of flow: a gas source connected with the gas expanding unit, the gas expanding unit connected with the swirl tube arrangement, the swirl tube arrangement connected with the liquid/gas separator.
  • the curved line forms a forms at least 20 % of the front end (in the direction of flow) of the fixing line, more preferably at least 30 % of the front end (in the direction of flow) of the fixing line, even more preferably forms at least 40 % of the front end (in the direction of flow) of the fixing line.
  • the inventive structure of the fixing line identical with the contact area of the vanes with the inner hubs enhances the coalescence of the liquid droplets within the gas stream.
  • no drainage slots are included in the swirl tube arrangement.
  • the swirl tube arrangement enhances the coalescence of the liquid droplets in the gas stream.
  • the liquid particles are not removed in the swirl tube arrangement but rather in further downstream units.
  • the omittance of drainage slots is due to the low liquid droplet content in many applications and the focus on liquid droplet grow. Therefore the swirl tube arrangement is especially suitable for high GVF (gas volume fraction), i.e. gas in which there is very little liquid so natural coalescing of liquid in the pipe doesn’t occur rapidly.
  • GVF gas volume fraction
  • the present invention further comprises a process for increasing the liquid droplet size in a gas stream and the subsequent liquid removal from a gas stream at least comprising the following steps.
  • a first liquid droplet containing gas stream from a gas source is introduced into a horizontally placed swirl tube arrangement connected upstream with the gas source.
  • the swirl tube arrangement at least comprises an outer pipe, an inner hub fixed within the outer pipe and four or more vanes attached to the inner hub.
  • the second liquid droplet containing gas stream is transferred into a liquid/gas separator and a third gas stream without liquid droplets or with a reduced amount of liquids droplets is obtained.
  • the first liquid droplet containing gas stream is introduced into a gas expanding unit before entering the swirl tube arrangement.
  • the gas expanding unit comprises a Joule-Thompson Valve. Due to the pressure drop, the gas stream is cooled which further supports the droplet coalescence behind (in the direction of flow) the vanes.
  • the first liquid droplet containing gas stream has a pressure in the range between 20 bar to 90 bar, preferably between 40 bar to 60 bar. All pressure ranges in the invention refer to absolute pressure.
  • the gas expanding unit induces a pressure drop of between 5 bar to 20 bar.
  • the gas processing arrangement for natural gas gathering and conditioning at least comprises a gas source and a horizontally placed swirl tube arrangement connected upstream with the gas source.
  • the swirl tube arrangement comprises an outer pipe, an inner hub fixed within the outer pipe and four or more vanes.
  • the inner hub is closed on both sides.
  • the vanes are attached to the inner hub along a fixing line comprising a curved line and a straight line and wherein the curved line forms at least 20 % of the fixing line.
  • the vanes comprise at least two sections.
  • the first section of the vane comprises a contact area with the inner hub, which is characterized in that the contact area can be defined by multiple parallel straight lines. This section is defined as a fixing line comprising a straight line.
  • the second section of the vane comprises a contact area with the inner hub, which is characterized in that the contact area can be defined by multiple parallel curved lines.
  • the term“multiple parallel straight or curved lines” depends on the thickness of the contact area of the vanes.
  • the curved line forms at least 30 %, more preferably 40 % to 60 % of the fixing line. More preferably the curved line is oriented at the front end (in the direction of flow) of the fixing line. Therefore, a gas stream passes at first through a first vane part with a curved basic geometry and afterwards a second vane part with a linear basic geometry.
  • basic geometry refers to the contact surface between the vane and the inner hub alongside the fixing line.
  • the vane angle a [alfa] of the straight line (as a part of the above described fixing line referring to the vane contact area with the inner hub) is in the range of (including) 20° [degrees] to 70° [degrees], more preferably in the range between (including) 40° [degrees] to 60° [degrees].
  • the term“vane angle” refers to the angle between a (virtual) line through the inner hub, located orthogonal to the inner central axis in the direction of flow and located and connected with the end point of the straight line.
  • the end point of the straight line refers to the end point of the respective vane, too.
  • the vane angle is further described and defined in figure 2.
  • the specific vane angle range supports and increases the coalescence of the liquid droplets in the gas stream within the outer pipe.
  • the vane angle is measured in an unfolded view as described in figure 2.
  • the vane overlap b [beta] of the straight line (as a part of the above described fixing line referring to the vane contact area with the inner hub) is in the range of 10° [degrees] to 40° [degrees], more preferably 20° [degrees] to 30 [degrees].
  • the vane overlap is measured as the smaller angle of a virtual parallelogram formed by two adjacent straight lines.
  • the vane overlap angle is measured in an unfolded view as described in figure 2.
  • Another aspect of the invention relates to the use of a gas processing arrangement as described above for the improvement of removal efficiency of fine liquid droplets in gas streams, preferably natural gas or synthesis gas.
  • Figure 1 shows a schematic view of a preferred embodiment of the gas processing arrangement according to the invention
  • Figure 2 shows a schematic two-dimensional view of the inner hub and unfolded vanes
  • Figure 3 shows a tridimensional view of a section of the swirl tube arrangement.
  • FIG. 1 shows a schematic view of a preferred embodiment of the gas processing arrangement according to the invention.
  • the swirl tube arrangement (6) is connected (upstream) with the gas source (5).
  • a gas expanding unit (7) is arranged between the gas source (5) and the swirl tube arrangement (6).
  • the gas expanding unit comprises a Joule- Thompson valve. Due to the pressure drop, the gas stream is cooled which further supports the liquid droplet coalescence behind (in the direction of flow) the vanes within the swirl tube arrangement (6).
  • the swirl tube arrangement (6) is connected (downstream) with a liquid/gas separator (7).
  • the swirl tube arrangement (6) enables liquid droplets grow based on droplet coalescence as described above. These grown droplets can be easily removed in the downstream liquid/gas separator (7). This includes the removal of very small droplets in a dry gas stream, e.g. below 0.5 wt. % water.
  • Figure 2 shows a schematic two-dimensional view of the inner hub (2) and unfolded vanes (3).
  • This figure shows the vanes in an unfolded view, e.g. before tac welding the vanes to the inner hub (2).
  • the angle a [alfa] is measured between the straight line (11 b) of the vane (3) and the base line (11 c) of the unfolded view.
  • the base line (11 c) marks the gas stream leaving the vanes (3) and is a virtual line connecting the end-points (in the flow direction (I) of the gas stream indicated as bold arrows) of the vanes vane (3).
  • the separating line (11 d) marks the end of the straight line (11 b) and the beginning of the curved line (11 a).
  • Figure 3 shows a tridimensional view of a section of the swirl tube arrangement (6).
  • the inner hub (2) is fixed (not shown) within the outer pipe (1 ).
  • the vanes (3) induce a vortex like gas stream resulting in a liquid droplet coalescence.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Cyclones (AREA)
  • Separating Particles In Gases By Inertia (AREA)

Abstract

L'invention concerne un agencement de traitement de gaz (I) pour la collecte et le conditionnement de gaz naturel comprenant au moins : - une source de gaz (5); - un agencement de tube tourbillonnant disposé horizontalement (6) raccordé en amont de la source de gaz (5), l'agencement de tube tourbillonnant (6) comprenant un tuyau externe (1), un moyeu interne (2) fixé à l'intérieur du tuyau externe (1) et quatre ou plusieurs pales (3) fixées au moyeu interne (2).
PCT/EP2018/072157 2018-08-15 2018-08-15 Dispositif à tube tourbillonnant en ligne pour la coalescence de gouttelettes liquides dans une application de gaz pauvre WO2020035139A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/EP2018/072157 WO2020035139A1 (fr) 2018-08-15 2018-08-15 Dispositif à tube tourbillonnant en ligne pour la coalescence de gouttelettes liquides dans une application de gaz pauvre

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2018/072157 WO2020035139A1 (fr) 2018-08-15 2018-08-15 Dispositif à tube tourbillonnant en ligne pour la coalescence de gouttelettes liquides dans une application de gaz pauvre

Publications (1)

Publication Number Publication Date
WO2020035139A1 true WO2020035139A1 (fr) 2020-02-20

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PCT/EP2018/072157 WO2020035139A1 (fr) 2018-08-15 2018-08-15 Dispositif à tube tourbillonnant en ligne pour la coalescence de gouttelettes liquides dans une application de gaz pauvre

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Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1043285B (de) 1953-08-10 1958-11-13 Otto & Co Gmbh Dr C Rohrfoermiger Fluessigkeitsabscheider fuer Gase und Daempfe
US3258895A (en) 1962-10-19 1966-07-05 Joy Mfg Co Device for separating solids from a gaseous medium
US5743926A (en) 1996-08-01 1998-04-28 Shell Oil Company Apparatus for separation of liquid and vapor in distillation/flashing process
WO1999003554A1 (fr) 1997-07-18 1999-01-28 Koch-Glitsch, Inc. Tube de venturi a effet de tourbillonnement pour plateau de contact vapeur-liquide
WO2001066225A2 (fr) 2000-03-08 2001-09-13 Shell Internationale Research Maatschappij B.V. Separateur vapeur/liquide
US6666338B1 (en) * 1998-12-15 2003-12-23 Vattenfall Ab Device for the separation of solid objects from a flowing fluid
US20100140187A1 (en) * 2007-01-11 2010-06-10 Schinfa Engineering Device and method for separating a flowing medium mixture with a stationary cyclone
US20110154856A1 (en) * 2008-07-10 2011-06-30 Diki Andrian Process for removing a gaseous contaminant from a contaminated gas stream
US20140116255A1 (en) * 2012-10-31 2014-05-01 Intevep, S.A. Axial gas-liquid cyclone separator

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1043285B (de) 1953-08-10 1958-11-13 Otto & Co Gmbh Dr C Rohrfoermiger Fluessigkeitsabscheider fuer Gase und Daempfe
US3258895A (en) 1962-10-19 1966-07-05 Joy Mfg Co Device for separating solids from a gaseous medium
US5743926A (en) 1996-08-01 1998-04-28 Shell Oil Company Apparatus for separation of liquid and vapor in distillation/flashing process
WO1999003554A1 (fr) 1997-07-18 1999-01-28 Koch-Glitsch, Inc. Tube de venturi a effet de tourbillonnement pour plateau de contact vapeur-liquide
US6666338B1 (en) * 1998-12-15 2003-12-23 Vattenfall Ab Device for the separation of solid objects from a flowing fluid
WO2001066225A2 (fr) 2000-03-08 2001-09-13 Shell Internationale Research Maatschappij B.V. Separateur vapeur/liquide
US20100140187A1 (en) * 2007-01-11 2010-06-10 Schinfa Engineering Device and method for separating a flowing medium mixture with a stationary cyclone
US20110154856A1 (en) * 2008-07-10 2011-06-30 Diki Andrian Process for removing a gaseous contaminant from a contaminated gas stream
US20140116255A1 (en) * 2012-10-31 2014-05-01 Intevep, S.A. Axial gas-liquid cyclone separator

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