WO2008088347A1 - Épurateur à fluide - Google Patents

Épurateur à fluide Download PDF

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Publication number
WO2008088347A1
WO2008088347A1 PCT/US2007/001633 US2007001633W WO2008088347A1 WO 2008088347 A1 WO2008088347 A1 WO 2008088347A1 US 2007001633 W US2007001633 W US 2007001633W WO 2008088347 A1 WO2008088347 A1 WO 2008088347A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
reaction vessel
fluid
weir
fluid scrubber
Prior art date
Application number
PCT/US2007/001633
Other languages
English (en)
Inventor
Bernard F. Duesel, Jr.
Michael J. Rutsch
Original Assignee
Duesel Bernard F Jr
Rutsch Michael J
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 Duesel Bernard F Jr, Rutsch Michael J filed Critical Duesel Bernard F Jr
Priority to PCT/US2007/001633 priority Critical patent/WO2008088347A1/fr
Publication of WO2008088347A1 publication Critical patent/WO2008088347A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • 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

  • Conventional spray tower fluid scrubbers typically use atomizing devices such as nozzles to disperse the scrubbing liquid as small droplets into a spray chamber.
  • atomizing devices such as nozzles
  • smaller droplet sizes of scrubbing liquid improve the efficiency of spray tower fluid scrubbers by increasing the available surface area for intimate contact between the scrubbing liquid and gas phases.
  • spray tower designs must strike a balance between the size of the atomized droplets and the energy requirements to first form very small droplets and then to separate such droplets from the flowing gas stream before the gas is discharged from the scrubber.
  • Spray tower fluid scrubbers usually require significant headspace to accommodate the height of the tower.
  • submerged gas reactors Like most fluid scrubbers, submerged gas reactors/evaporators (hereinafter “submerged gas reactors”) generally mix liquids and gasses. However, unlike most conventional fluid scrubbers, within submerged gas reactors a discontinuous gas phase is dispersed within a continuous liquid phase. Submerged gas reactors are used in many industries to perform chemical reaction processes with respect to various constituents.
  • U.S. Patent No. 5,342,482 which is hereby incorporated by reference, discloses a common type of submerged gas reactor in which combustion gas is generated and delivered though an inlet pipe to a dispersal unit submerged within the liquid to be reacted.
  • the required volume of the gas-liquid contact zone is the minimum possible and generally a much smaller volume than that required in conventional spray tower and packed tower fluid scrubbers, thus favoring more compact designs compared to spray tower and packed tower scrubbers.
  • demisters employed for separating entrained liquid droplets from the gas phase within submerged gas reactors typically consume significantly less energy than the demister sections required for venturi fluid scrubbers and somewhat less energy than demisters used in spray tower and packed tower fluid scrubbers.
  • polluted gas introduced through each tube mixes with the scrubbing liquid in a first confined volume formed by each weir, or each weir and walls of the vessel, and the tube(s), and the mixture of gas and liquid flows at high volume with a high degree of turbulence along the circulation path defined around each weir, thereby causing a high degree of mixing between the gas and the scrubbing liquid and any suspended particles within the scrubbing liquid.
  • the predominantly horizontal flow direction of the liquid and gas mixture over the top of the weir and along the surface of the scrubbing liquid within the reaction vessel enables the gas phase to disengage from the scrubbing liquid with minimal entrainment of liquid due to the significantly greater momentum of the much higher density liquid that is directed primarily horizontally compared to the low density gas with a relatively weak but constant vertical momentum component due to buoyancy.
  • Fig. 1 is a cross-sectional view of a fluid scrubber in accordance with the teachings of the disclosure.
  • Fig. 3 is a cross-sectional view of a third fluid scrubber having a tubular shaped weir.
  • Fig. 4 is a top plan view of the fluid scrubber of Fig. 3.
  • Fig. 5 is a cross-sectional view of a fourth fluid scrubber connected to a source of waste heat.
  • the performance of fluid scrubbers according to the disclosure depends on the properties of the pollutant(s) to be removed from the gas feed stream, the properties of the scrubbing liquid and the temperature and humidity of the gas feed stream.
  • the gas feed stream is contaminated industrial exhaust.
  • fluid scrubbers according to the disclosure may be realized by substituting such fluid scrubbers for conventional fluid scrubbers in almost any fluid scrubbing application.
  • conventional means may be employed to control the flow of contaminated gas and scrubbing liquid through the fluid scrubber and, if required, to post-treat the liquid and/or gas streams.
  • a scrubbing liquid inlet port 34 is disposed in one side of the reactor vessel 30 and enables a scrubbing liquid 35 (and other liquids) to be provided into the interior of the reactor vessel 30.
  • a weir 40 which is illustrated in Fig. 1 as a flat or solid plate member having a first or lower end 41 and a second or upper end 42, is disposed within the reactor vessel 30 adjacent the gas inlet tube 22. The weir 40 defines and separates two volumes 70 and 71 within the reactor vessel 30.
  • a gas exit port 60 disposed in the top of the reaction vessel 30, enables gas to exit from the interior of the reaction vessel 30.
  • a blower 20 (in this case an induction fan) is disposed on the gas exit port 60 in this embodiment, thus providing gas to the reaction vessel 30.
  • a demister 61 Disposed at or near a junction of the gas exit port 60 and the reaction vessel 30 is a demister 61.
  • the demister 61 removes droplets of scrubbing liquid that are entrained in the gas phase as the gas disengages from the liquid phase at a surface 80 of the scrubbing liquid.
  • the demister 61 may be a vane-type demister, a mesh pad-type demister, or any combination of commercially available demister elements. Further, a vane-type demister may be provided having a coalescing filter to improve demisting performance.
  • the demister 61 may be mounted in any orientation and adapted to a particular vessel 30 including, but not limited to, horizontal and vertical orientations.
  • the blower 20 provides polluted gas to the vessel 30 by drawing the gas from a source (not shown) through a line 51, the gas inlet tube 22 and the gas exit ports 24 into the interior of vessel 30.
  • a blower disposed on the inlet gas side of the system could be used to deliver the polluted gas under pressure into the interior of reaction vessel 30 instead of drawing the polluted gas into the reaction vessel 30 with the induction fan/blower 20.
  • the scrubbing liquid 35 may be supplied through the scrubbing liquid inlet 34 by a pump (not shown in Fig.
  • a level sensor and control (not shown in Fig. 1) may be used to determine and control the rate that the scrubbing liquid 35 is supplied through the inlet port 34.
  • the weir 40 is mounted within the reaction vessel 30 to form a lower circulation gap 36 between the first end 41 of the weir 40 and the bottom wall 31 of the reaction vessel 30 and to form an upper circulation gap 37 between the second end 42 of the weir 40 and the surface 80 of the scrubbing liquid 35 (or the top wall of the reaction vessel 30).
  • the upper end 42 of the weir 40 is preferably set to be at or below the surface 80 of the scrubbing liquid 35 when the scrubbing liquid 35 is at rest (i.e., when no gas is being introduced into the reaction vessel via the gas inlet tube 22).
  • the weir 40 also defines and separates the confined volume or space 70 in which the sparge ports 24 are located from the volume or space 71.
  • the weir 40 may be mounted to the reaction vessel 30 via welding, bolts or other fasteners attached to internal side walls of the reaction vessel 30.
  • a polluted gas is induced to flow under negative pressure created by the blower 20 into and through the gas inlet tube 22 before reaching the sparge or exit ports 24.
  • the gas exits the gas inlet tube 22 through the sparge ports 24 into the confined volume 70 formed between the weir 40 and the gas inlet tube 22, causing the gas to be dispersed into the continuous liquid phase of the scrubbing liquid within the reaction vessel 30.
  • gas exiting from the sparge ports 24 mixes with the liquid phase of the scrubbing liquid within the confined volume 70 and causes a high volume flow pattern to develop around the weir 40.
  • the velocity of the flow pattern and hence the turbulence associated with the flow pattern is highest within the confined volume 70 and at the locations where the liquid flows through the upper gap 37 and the lower gap 36 of the weir 40.
  • the turbulence within the confined volume 70 significantly enhances the dispersion of the gas into the scrubbing liquid which, in turn, provides for efficient heat and mass transfer between the gas and the scrubbing liquid.
  • the gas is dispersed as a discontinuous phase into a continuous liquid phase of the scrubbing liquid forming a gas/liquid mixture within the confined volume 70.
  • the mass per unit volume of the gas/liquid mixture in the confined volume 70 is significantly less than the average mass per unit volume of the mixture of gas and scrubbing liquid in the volume 71. Due to this large difference in mass per unit volume of the liquid compared to the gas, typically on the order of approximately 1000 to 1, a difference in static hydraulic pressure is formed between the gas/liquid mixture in the confined volume 70 and the liquid phase in the volume 71 at all elevations. This imbalance in static hydraulic pressure forces the scrubbing liquid to flow from the higher pressure region, i.e., the volume 71 , to the lower pressure region, i.e., the confined volume 70, at a rate that overcomes the impressed static hydraulic pressure imbalance and creates flow upward through the confined volume 70.
  • the dispersion of gas into the scrubbing liquid 35 within the confined volume 70 at the sparge ports 24 develops a continuous flow pattern that draws scrubbing liquid 35 under the bottom edge 41 of the weir 40 through the lower circulation gap 36, and causes the mixture of gas and scrubbing liquid 35 to move through the confined volume 70 and toward the surface 80 of the scrubbing liquid 35.
  • the gas/liquid mixture reaches a point of balance at which the imbalance of static hydraulic pressure is eliminated. Generally speaking, this point is at or near the upper circulation gap 37 formed between the second end 42 of the weir 40 and the s surface 80.
  • the force of gravity which becomes the primary outside force acting on the gas/fluid mixture, gradually eliminates most of the vertical momentum component of the gas/liquid mixture.
  • This reduced vertical momentum causes the gas/liquid mixture to flow in a predominantly horizontal direction over the second end 42 of the weir 40 (through the circulation gap 37 defined at or near the surface 80 of the scrubbing liquid 35) and into the liquid phase of the scrubbing liquid 35 within the volume 71.
  • This flow pattern around the weir 40 affects the dispersion of the gas into the continuous liquid phase of the scrubbing liquid 35 and, in particular, thoroughly agitates the continuous liquid phase of the scrubbing liquid 35 within the reaction vessel 30 while creating a substantially horizontal flow pattern of the gas/liquid mixture at or near the surface 80 of the continuous liquid phase of the scrubbing liquid 35.
  • This horizontal flow pattern significantly mitigates the potential for entrained liquid droplets to be carried vertically upward along with the dispersed gas phase as the dispersed gas phase rises through the liquid phase due to buoyancy and finally disengages from the continuous liquid phase of the scrubbing liquid at the surface 80.
  • the mixing action within reaction vessel 30 helps to ensure that suspended particles formed in the fluid scrubbing process may be maintained in suspension within the liquid phase circulating around the weir 40, which effectively mitigates the formation of blockages and fouling within the fluid scrubber.
  • the efficiency of the fluid scrubber is improved over known fluid scrubbing systems in terms of freedom from clogging and fouling.
  • fluid scrubbing is a process that affects mass transfer of pollutants from a polluted gas stream and sequesters the pollutant within a scrubbing liquid by causing the polluted gas and scrubbing liquid to be brought into intimate contact for a finite period of time.
  • the scrubbing liquid which can be a solution or slurry, may contain one or more reagents that react chemically with one or more of targeted pollutants within gas. Through appropriate chemical reactions, targeted pollutants can frequently be turned into less noxious compounds, and these less noxious compounds remain sequestered within the scrubbing liquid.
  • a fluid scrubber configured as a submerged gas reactor
  • heat and mass transfer and chemical reactions occur simultaneously at the interface formed by the dynamic boundaries of the discontinuous gas and continuous liquid phases.
  • the system shown in Fig. 1 integrates the functions of dispersing the gas into the liquid phase, providing thorough agitation of the liquid phase, and mitigating entrainment of liquid droplets with the gas phase as the gas disengages from the liquid. Additionally, the turbulence and mixing that occurs within the reaction vessel 30 due to the flow pattern created by dispersion of gas into liquid within the confined volume 70 reduces the formation of large crystals of precipitates and/or large agglomerates of smaller particles within the reaction vessel 30.
  • Fig. 2 illustrates a second embodiment of a fluid scrubber 110, which is very similar to the fluid scrubber 10 of Fig. 1 and in which elements shown in Fig. 2 are assigned reference numbers being exactly 100 greater than the corresponding elements of Fig. 1.
  • the fluid scrubber 110 includes a baffle or a shield 138 disposed within the reaction vessel 130 at a location slightly above or slightly below the scrubbing liquid surface 180 and above the second end 142 of the weir 140.
  • the baffle or shield 138 may be shaped and sized to conform generally to the horizontal cross-sectional area of the confined volume 170.
  • weirs 40 and 140 preferably extend across the reaction vessels 30 and 130 between opposite walls of the reaction vessels 30 and 130, they may be formed into any desired shape so long as a substantial barrier is formed to isolate one volume 70 (or 170) closest to the gas inlet tube 22 from the volume 71 (or 171) on the opposite side of the weir 40, 140.
  • the dimensions of the fluid scrubber 210 are exemplary only, the ratios between these dimensions may serve as a guide for those skilled in the art to achieve a desirable balance between three desirable process results including: 1) preventing the formation of large crystals of precipitates and/or agglomerates of solid particles while maintaining solid particles as a homogeneous suspension within the scrubbing liquid by controlling the degree of overall mixing within reaction vessel 230; 2) enhancing the rates of heat and mass transfer and desirable chemical reactions by controlling the turbulence and hence interfacial surface area created between the gas and liquid phases within confined volume 270; and 3) mitigating the potential of entraining liquid droplets in the gas as the gas stream disengages from the liquid phase at the scrubbing liquid surface 280 by maintaining a desirable and predominately horizontal velocity component for the gas/liquid mixture flowing outward over the second end 242 of the weir 240 and along the surface 280 within reaction vessel 230.
  • the fluid scrubber 210 includes a reaction vessel 230 with a dished bottom having an interior volume and a vertical gas inlet tube 222 at least partially disposed within the interior volume of the reaction vessel 230.
  • the gas inlet tube 222 has a diameter of approximately 20 inches and the overall diameter of the reaction vessel 230 is approximately 120 inches, but these diameters may be more or less based on the design capacity and desired process result as relates to both gas and liquid flow rates and the type of combustion device (not shown in Fig 3) supplying gas to the fluid scrubber.
  • the weir 240 has a diameter of approximately 40 inches with vertical walls approximately 26 inches in length.
  • the combustion gas exits the gas inlet tube 222 through the sparge ports 224 into a confined volume 270 formed between the gas inlet tube 222 and a tubular shaped weir 240.
  • the weir 240 has a circular cross-sectional shape and encircles the lower end of the gas inlet tube 222. Additionally, the weir 240 is located at an elevation which creates a lower circulation gap 236 of approximately 4.inches between a first end 241 of the weir 240 and a bottom dished surface 231 of the reaction vessel 230.
  • Several support brackets 233 are mounted to the bottom surface 231 of the reaction vessel 230 and are attached to the weir 240 near the first end 241 of the weir 240. Additionally, a gas inlet tube stabilizer ring 235 is attached to the support brackets 233 and substantially surrounds the bottom end 226 of the gas inlet tube 222 to stabilize the gas inlet tube 222 during operation.
  • the induced flow pattern and resultant vigorous mixing action creates significant shearing forces that are primarily based on the difference in specific gravity and hence momentum vectors between the liquid and gas phases at all points on the interfacial surface area of the liquid and gas phases.
  • the shearing forces driven by the significant difference in specific gravity between the liquid and gas phases which is, generally speaking, of a magnitude of 1000:1 liquid to gas, cause the interfacial surface area between the gas and liquid phases to increase significantly as the average volume of each discrete gas region within the mixture becomes smaller and smaller due to the shearing force of the flowing liquid phase.
  • the horizontal velocity component continually decreases causing a continual reduction in momentum and a reduction of the resultant shearing forces acting at the interfacial area within the gas/liquid mixture.
  • the reduction in momentum and resultant shearing forces allows the force of buoyancy to become the primary driving force directing the movement of the discontinuous gas regions within the gas/liquid mixture, which causes discrete and discontinuous regions of gas to coalesce while ascending vertically within the continuous liquid phase.
  • the shape of the cross sectional area and length of the gas inlet tube is generally set by the allowable pressure drop, the configuration of the reaction vessel, and the costs of forming suitable material to match the desired cross sectional area, and, importantly, if direct fired, the characteristics of the burner that is coupled to the fluid scrubber.
  • the vertical distance between the top edge 242 of the weir 240 and the top edge of the sparge ports should be not less than about 6 inches and preferably is at least about 17 inches.
  • Selecting the shape and, more particularly, the size of the sparge port 224 openings is a balance between allowable pressure drop and the initial amount of interfacial area created at the point where the gas is dispersed into the flowing liquid phase within confined volume 271.
  • the open area of the sparge ports 224 is generally more important than the shape, which can be most any configuration including, but not limited to, rectangular, trapezoidal, triangular, round, oval.
  • the open area of the sparge ports 224 should be such that the ratio of gas flow to total combined open area of all sparge ports should at least be in the range of 1,000 to 18,000 acfm per ft 2 , preferably in the range of 2,000 to 10,000 acfm/ft 2 and more preferably in the range of 4,000 to 8,000 acfm/ft 2 , where acfm is referenced to the operating temperature within the gas inlet tube.
  • the ratio of the gas flow to the cross sectional area of the confined volume 270 (CSA co ⁇ ⁇ n ed v o )u me ) should be at least in the range of 400 to 10,000 scfm/ft 2 , preferably in the range of 500 to 4,000 scfm/ft 2 and more preferably in the range of 500 to 2,000 scfm/ft 2 .
  • weirs illustrated herein have been shown as flat plates or as tubular members having a circular cross-sectional shape, weirs of other shapes or configurations could be used as well, including weirs having a square, rectangular, oval, or other cross sectional shape disposed around a fire or other gas inlet tube, weirs being curved, arcuate, or multi-faceted in shape or having one or more walls disposed partially around a fire or gas inlet tube, etc.
  • the gas entry ports shown as rectangular may assume most any shape including trapezoidal, triangular, circular, oval, or triangular.
  • the weirs need not be solid surfaces and may be perforated or latticed if desired.
  • the fluid scrubbers described herein may be operated in continuous, batch or combined continuous ' and batch modes.
  • the fluid scrubber may be initially charged with a controlled amount of scrubbing liquid and operated in a batch mode.
  • liquid feed is continuously added to the fluid scrubber to maintain a constant predetermined level within the reaction vessel by replacing any components of the scrubbing liquid that are evaporated and/or reacted as the process proceeds.

Abstract

L'invention concerne un épurateur à fluide sous forme de réacteur à gaz submergé, comprenant une cuve de réaction, un tube de distribution de gaz partiellement disposé dans la cuve de réaction, conçu pour introduire un gaz dans la cuve de réaction, ainsi qu'une prise d'eau d'épuration permettant d'introduire un liquide d'épuration dans la cuve de réaction avec un débit suffisant pour maintenir un niveau constant d'eau dans la cuve de réaction. Un déversoir est disposé dans la cuve de réaction, à proximité du tube de distribution de gaz, de manière à former un premier circuit d'écoulement entre une première extrémité du déversoir et une paroi de la cuve de réaction et un second circuit d'écoulement entre une seconde extrémité du déversoir et une extrémité supérieure de la cuve de réaction. Dans la pratique, le gaz introduit par le tube se mélange au liquide d'épuration et le mélange gaz-eau circule avec un débit élevé et un niveau de turbulence élevé par le premier et le second circuit d'écoulement formés autour du déversoir, ce qui permet de mélanger vigoureusement le gaz et l'eau. Cet écoulement turbulent permet d'obtenir une surface interfaciale importante entre l'eau et le gaz, ce qui entraîne une réduction du temps de séjour nécessaire du gaz dans le liquide d'épuration pour obtenir un équilibre thermique et/ou pour mener à terme des réactions chimiques, tout ceci conduisant à une évaporation, à une réaction chimique, ou à une évaporation et à une réaction chimique combinées plus efficace et complète.
PCT/US2007/001633 2007-01-19 2007-01-19 Épurateur à fluide WO2008088347A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/US2007/001633 WO2008088347A1 (fr) 2007-01-19 2007-01-19 Épurateur à fluide

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/US2007/001633 WO2008088347A1 (fr) 2007-01-19 2007-01-19 Épurateur à fluide

Publications (1)

Publication Number Publication Date
WO2008088347A1 true WO2008088347A1 (fr) 2008-07-24

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PCT/US2007/001633 WO2008088347A1 (fr) 2007-01-19 2007-01-19 Épurateur à fluide

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WO (1) WO2008088347A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108704436A (zh) * 2018-06-11 2018-10-26 广州引航者信息科技有限公司 一种用于船舶舱生产的空气净化装置

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4060587A (en) * 1975-06-30 1977-11-29 National Lime Association Gaseous and liquid reactant treatment
US20040213721A1 (en) * 1997-05-16 2004-10-28 Arno Jose I Apparatus and method for point-of-use treatment of effluent gas streams
US7144555B1 (en) * 2001-06-20 2006-12-05 Well To Wire Emissions Control Inc. Method and apparatus for hydrogen sulphide removal

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4060587A (en) * 1975-06-30 1977-11-29 National Lime Association Gaseous and liquid reactant treatment
US20040213721A1 (en) * 1997-05-16 2004-10-28 Arno Jose I Apparatus and method for point-of-use treatment of effluent gas streams
US7144555B1 (en) * 2001-06-20 2006-12-05 Well To Wire Emissions Control Inc. Method and apparatus for hydrogen sulphide removal

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108704436A (zh) * 2018-06-11 2018-10-26 广州引航者信息科技有限公司 一种用于船舶舱生产的空气净化装置

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