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WO2009114571A2 - Système et procédé d'oxydation thermique sans flamme à des rapports d'équivalence optimisés - Google Patents

Système et procédé d'oxydation thermique sans flamme à des rapports d'équivalence optimisés Download PDF

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Publication number
WO2009114571A2
WO2009114571A2 PCT/US2009/036724 US2009036724W WO2009114571A2 WO 2009114571 A2 WO2009114571 A2 WO 2009114571A2 US 2009036724 W US2009036724 W US 2009036724W WO 2009114571 A2 WO2009114571 A2 WO 2009114571A2
Authority
WO
WIPO (PCT)
Prior art keywords
fuel
conduit
mixing
matrix bed
oxidizing agent
Prior art date
Application number
PCT/US2009/036724
Other languages
English (en)
Other versions
WO2009114571A3 (fr
Inventor
Peter Falcone
Original Assignee
Selas Fluid Processing Corporation
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 Selas Fluid Processing Corporation filed Critical Selas Fluid Processing Corporation
Priority to US12/921,481 priority Critical patent/US20110283991A1/en
Publication of WO2009114571A2 publication Critical patent/WO2009114571A2/fr
Publication of WO2009114571A3 publication Critical patent/WO2009114571A3/fr
Priority to US14/298,019 priority patent/US9970683B2/en
Priority to US15/947,988 priority patent/US10234174B2/en

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0285—Heating or cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • B01J8/0257—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical annular shaped bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0278—Feeding reactive fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • F23G7/061—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating
    • F23G7/065—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating using gaseous or liquid fuel
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00044—Temperature measurement
    • B01J2208/00061—Temperature measurement of the reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00477—Controlling the temperature by thermal insulation means
    • B01J2208/00495—Controlling the temperature by thermal insulation means using insulating materials or refractories
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00504—Controlling the temperature by means of a burner
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00513—Controlling the temperature using inert heat absorbing solids in the bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/19—Details relating to the geometry of the reactor
    • B01J2219/194—Details relating to the geometry of the reactor round
    • B01J2219/1941—Details relating to the geometry of the reactor round circular or disk-shaped
    • B01J2219/1943—Details relating to the geometry of the reactor round circular or disk-shaped cylindrical
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/50—Combustion in a matrix bed combustion chamber

Definitions

  • the present invention relates to a flameless thermal oxidizer configured for flameless thermal oxidation at optimized equivalence ratios, and a method of flameless thermal oxidation at optimized equivalence ratios.
  • react or “reaction” refer to any endothermic or exothermic chemical reaction, such as the vaporization, synthesis, oxidation, or reduction of a chemical.
  • LNG liquid natural gas
  • chemicals and fume streams may be safely destroyed through oxidation by converting the chemical to reaction products, such as carbon dioxide and water.
  • Thermal oxidation is a process whereby solvents and hydrocarbons combine with oxygen to form water and carbon dioxide. The products of reaction from the original mixture of solvents can thereafter be safely discharged to the atmosphere.
  • FTO flameless thermal oxidizer
  • the reaction is referred to as 'flameless' because the FTO permits the reaction of the process gas stream to occur in the absence of a flame.
  • the flameless thermal oxidizer may be utilized, for example, to treat organic vent gases released from organic synthesis reactors and similar hydrocarbon off-gas control applications, to vaporize liquid natural gas, or to synthesize waste hydrocarbon gas or natural gas feedstock through a non-catalytic, partial oxidation process. Flameless thermal oxidizers are described, for example, in U.S. Pat. No. 6,015,540 to McAdams et al., which is incorporated herein by reference in its entirety.
  • FIG. 1 is a schematic cross-sectional view of a flameless thermal oxidizer (FTO).
  • FTO flameless thermal oxidizer
  • FIG. 2 is a schematic cross-sectional view of an FTO including a diptube assembly according to an exemplary embodiment of the invention
  • FIG. 3 is a detailed cross-sectional view of the diptube assembly of FIG. 2;
  • FIG. 4 is a top plan view of the diptube assembly taken along the lines 4-4 of FIG. 2;
  • FIG. 5 is a detailed cross-sectional view of a mixing conduit of FIG. 3 according to an exemplary embodiment of the invention.
  • FIG. 6A is a detailed cross-sectional view of the mixing conduit of FIG. 5 taken along the lines 6-6; and FIG. 6B is another detailed cross-sectional view of a mixing conduit according to another exemplary embodiment of the invention, wherein the apertures of the mixing tube are disposed at alternate positions.
  • FIG. 1 depicts a flameless thermal oxidizer (FTO) 40 shown schematically.
  • the FTO operates by thermally reacting a process gas stream within a matrix bed of porous inert media (PIM).
  • PIM porous inert media
  • the FTO 40 includes a vessel 41 filled with a matrix bed of PIM 42 (a small portion of the PIM matrix bed is illustrated).
  • the PIM may be, for example, a packed bed of heat resistant material, such as ceramic balls or saddles.
  • the matrix bed 42 is heated by introducing a heated medium 48 (for example, air or flue gases generated by a fuel gas burner or an electric resistance heater) through a heating inlet 49.
  • a reactable process stream 44 is delivered into the heated matrix bed to facilitate an oxidation reaction.
  • the reactable process stream 44 is formed by combining a fume stream 51 containing an oxidizable material, an oxidizing agent stream 52 (such as air or oxygen), and a supplementary fuel gas stream 53 in a mixing device 50.
  • the oxidizing agent 52 and supplementary fuel 51 promote oxidation of the fume stream 51.
  • the diptube 43 is an open pipe of substantially constant inner and outer diameter, which extends at least partially within the PIM matrix bed 42, as shown.
  • the diptube 43 has an inlet 54 configured to receive the reactable process stream 44 and an outlet 55 configured to deliver the air-combustible vapor mixture into the matrix bed 42.
  • the reactable process stream 44 is directed into a region of the PIM matrix bed 42 where the matrix bed temperature is sufficient to react the process stream to form at least one reaction wave 56.
  • the chemicals in the process stream typically remain substantially unreacted until reaching the reaction wave 56, where a substantial portion of the chemicals are reacted over the wave length.
  • the non-planar reaction wave 56 is established entirely within the boundaries of the matrix bed.
  • the reactable process stream 44 is reacted in the reaction wave 56 to produce the reacted process stream 46.
  • the reacted process stream 46 is then directed through the matrix bed 42, through the void space 47, and out of the vessel through the exhaust outlet 45.
  • the location, stability, and size of the reaction wave 56 may be controlled through a programmable control system 59.
  • control system 59 that uses the readings from temperature sensors 58 to adjust the flow rates of the fume stream 51, oxidizing agent stream 52, and supplementary fuel gas stream 53. For example, if the temperature declines in a specified location of the matrix bed, the control system 59 is configured to send a signal, such as an electrical or pneumatic signal, to a series of control valves (not shown) to increase the flow rate of supplemental fuel 53, or to decrease the flow rate of the oxidizing agent 52 added to the flameless thermal oxidizer in order to prevent migration of the wave further away from the exit of the diptube.
  • a signal such as an electrical or pneumatic signal
  • control system 59 is configured to send a signal to a control valve (not shown) to decrease the flow rate of supplemental fuel 53 or increase the flow rate of the oxidizing agent 52 added to the flameless thermal oxidizer in order to prevent the wave from migrating into the inside of the diptube.
  • the control system 59 is also configured to adjust the flow rates of the fume stream 51, oxidizing agent stream 52, and supplementary fuel gas stream 53 in order to limit or prevent flashback. Flashback is a phenomena which occurs when the flame speed of a flammable mixture of fuel and air is greater than the local velocity profile of the flammable mixture in the presence of an ignition source.
  • the FTO 40 is not generally intended for use with a flammable gas mixture because it does not include provisions to contain flashback.
  • the FTO includes provisions, i.e., the programmable control system 59, for preventing flashback.
  • the mixture of the process gas stream 51, oxidizing agent stream 52 and supplementary fuel gas stream 53 is typically maintained at least about five percentage points below the lower flammability limit and delivered into the matrix bed at a velocity that is slightly greater than the flame speed of the mixture.
  • FIG. 2 depicts an exemplary embodiment of a flameless thermal oxidizer (FTO) 140 shown schematically according to aspects of the invention.
  • the FTO 140 is similar to the FTO 40 shown in FIG. 1, however, the diptube 43 and mixing device 50 of FIG. 1 are replaced with a diptube assembly 10. Similar to the diptube 43 of FIG. 1, the diptube assembly 10 is positioned at least partially within a PIM matrix bed 42 contained within the FTO vessel 41.
  • the diptube assembly 10 may be sized to fit within the same space constraints of the FTO vessel 41 as the diptube shown in FIG. 1.
  • the diptube assembly 10 generally comprises an outer conduit 12, a fuel conduit 14 positioned within the outer conduit 12, a fuel plenum 16 positioned at the base of the fuel conduit 14, and a plurality of mixing conduits 18 (one shown) extending through the fuel plenum 16. Only one mixing conduit 18 is shown throughout the figures for the purpose of clarity.
  • a mixture 19 comprising a fume stream and an oxidizing agent stream (e.g., oxygen or air) is introduced through an inlet 20 provided near the top end of outer conduit 12.
  • the fume stream and the oxidizing agent stream may either be combined at the inlet 20 of the outer conduit 12 or any other location.
  • the mixture 19 travels within the annular space defined between the outer conduit 12 and the fuel conduit 14. The mixture 19 is ultimately distributed into the individual mixing conduits 18.
  • a supplementary fuel stream 15 (e.g., natural gas, propane, kerosene, or #2 fuel oil) is introduced through an inlet 13 of the fuel conduit 14.
  • the fuel stream 15 travels along the fuel conduit 14 and is distributed into a fuel plenum 16.
  • the fuel plenum 16 is essentially a hollow cylinder defining a closed cylindrical region, through which the plurality of mixing conduits 18 are positioned.
  • the fuel stream 15 and the mixture 19 are isolated until they are combined together within the interior of the mixing conduits 18 (one shown in FIG. 3 for clarity) to form reactable process stream 32, as best described in FIG. 5.
  • FIG. 3 is a detailed view of the lower end of the diptube assembly 10 cross- section shown in FIG. 2, according to an exemplary embodiment of the invention.
  • FIG. 3 depicts a cross section of the outer conduit 12, fuel conduit 14, fuel plenum 16 and mixing conduits 18 (one shown for the purposes of clarity).
  • the fuel plenum 16 is mounted to the interior revolved surface of outer conduit 12.
  • the fuel plenum 16 may be welded, adhered or fastened, for example, to the interior surface of the outer conduit 12.
  • the fuel plenum 16 comprises an upper barrier 23, a lower barrier 24, and a cylindrical ring 25 interposed between the barriers 23 and 24.
  • the components of the fuel plenum 16 are optionally welded together.
  • the lower barrier 24 is a cylindrical disc having a series of holes formed therein for accommodating the mixing conduits 18, according to an exemplary embodiment of the invention.
  • the mixing conduits 18 may be welded to the lower barrier 24 to limit escapement of the fuel stream 15 through the lower barrier 24.
  • the upper barrier 23 is a cylindrical disc having a series of holes formed therein for accommodating the outlet end 26 of the fuel conduit 14 and the inlet end of each mixing conduit 18, as best shown in FIGS. 3 and 4.
  • FIG. 4 is a cross sectional view of the entire diptube assembly 10 taken along the lines 4-4 of FIG. 2.
  • the inlet end of each mixing conduit 18 is coupled to the upper barrier 23, and may be welded to the upper barrier 23 to limit or prevent introduction of the mixture 19 into the fuel plenum 16.
  • the outlet end 26 of the fuel conduit 14 is also coupled to the upper barrier 23, and may be welded to the upper barrier 23 to limit introduction of the fuel stream 15 into the annular space between the outer conduit 12 and the fuel conduit 14. Alternatively, it may be desirous to permit some portion of fuel stream 15 to mix into the annular space between the outer conduit 12 and the fuel conduit 14.
  • FIG. 5 depicts a detailed view of the mixing conduit 18 shown in FIG. 3.
  • the supplementary fuel stream 15 travels along the length of fuel conduit 14 and is distributed through the outlet end 26 of the fuel conduit 14 and into the fuel plenum 16.
  • the outlet end 26 of the fuel conduit 14 is mounted to a cylindrical opening provided in the upper barrier 23.
  • the fuel stream 15 collects in the fuel plenum 16 and is ultimately distributed into the mixing conduits 18 through a series of openings or apertures 30 formed along the surface of the mixing conduits 18.
  • the apertures 30 are formed along the segment of each mixing conduit 18 that is disposed between the upper and lower barriers 23 and 24, such that the fuel stream 15 within the fuel plenum 16 circulates into the mixing conduits 18. As best shown in FIG.
  • the fuel stream 15 is combined with the mixture 19 (comprising a fume stream and an optional oxidizing agent stream) within the mixing conduits 18 to form reactable process stream 32.
  • the reactable process stream 32 is ultimately delivered into the heated PIM matrix bed (not shown) through the outlet 22 of each mixing conduit 18.
  • the mixing conduits 18 are tailored to deliver the reactable process stream 32 into the PIM matrix bed with sufficient local velocity to limit or prevent a flashback. Flashbacks occur when the flame speed of a flammable mixture of fuel and air is greater than the local velocity profile of the fuel and air mixture in the presence of an ignition source. Accordingly, the potential for flashback is substantially reduced by increasing the local velocity profile of the fuel and air mixture, and quickly distributing that mixture into the matrix bed.
  • Substantially increasing the velocity of the reactable process stream reduces the residence time for a fully integrated fuel-air mixture within the mixing conduits 18, which diminishes the potential for uncontrolled deflagration due to inventory minimization of potentially combustible gases.
  • the fuel-air mixture may be maintained at or near the lower flammability limit of the mixture. Maintaining the fuel-air mixture at or near the lower flammability limit of the mixture minimizes FTO operational costs and maximizes the available capacity of the FTO vessel.
  • the number, position, cross-sectional area and length of the mixing conduits 18, individually or in combination, are tailored to deliver the reactable process stream 32 into the PIM matrix bed with sufficient local velocity to limit or prevent a flashback.
  • the collective cross-sectional area of the mixing conduits 18 is less than both the cross-sectional area of the fuel conduit 14 and the effective cross-sectional area of the outer conduit 12. Constricting the flow path of the mixture 19 through the mixing conduits 18 increases its local velocity, such that the local velocity of the mixture 19 (as it forms reactable process stream 32) is greater than its flame speed.
  • the collective cross-sectional area of the mixing conduits 18 is the sum of the interior cross-sectional areas of all of the mixing conduits 18.
  • the effective cross-sectional area of the outer conduit 12 is the difference between the interior cross-sectional area of the outer conduit 12 and the outer cross-sectional area of the fuel conduit 14, because the mixture 19 flows in the annular area defined between the outer conduit 12 and the fuel conduit 14.
  • the inner diameter of each mixing conduit 18 may be from about 0.5 to about 3 inches, for example.
  • the mixing conduit 10 may optionally include forty-two (42) mixing conduits 18.
  • the inner diameter of the outer conduit 12 may be from about 6 to about 60 inches, for example.
  • the inner diameter of the fuel conduit 14 that is positioned within the outer conduit may be from about 1 inch to about 6 inches, for example.
  • a ratio of the effective cross-sectional area of the outer conduit 12 to the collective cross-sectional of the mixing conduits 18 is between about 2.5:1 and 6: 1.
  • the velocity of the reactable process stream 32 increases as it travels through each mixing conduit 18.
  • the velocity of the reactable process stream 32 may be between about 50 feet/second to about 250 ft/second as it travels through each mixing conduit 18. Accordingly, the length of each mixing conduit 18 is maintained at a minimum such that the local velocity of the reactable process stream 32 is greater than its flame speed. According to one exemplary embodiment, for example, the length of each mixing conduit 18 may be about 36 inches. Minimizing the flow path of the reactable process stream 32 reduces the potential for substantial deceleration of the mixture 32 within each mixing conduit 18.
  • the distance separating the outlet of each mixing conduit 18 and the PIM of the matrix bed 42 is also maintained at a minimum to limit or prevent substantial deceleration of the reactable process stream 32 upon exiting the mixing conduit 18, but prior to reaching the PIM matrix bed 42.
  • the outlet of each mixing conduit 18 may be positioned within the matrix bed 42, if so desired.
  • each mixing conduit 18 is configured to premix the fuel stream 15 and the mixture 19 (containing air) at an equivalence ratio of between a range of about 0.5: 1 to about 0.8:1.
  • the equivalence ratio of the reactable process stream 32 may be maintained above the lower flammability limit for natural gas mixtures, i.e., above 0.4:1. Broadly stated, the equivalence ratio of the reactable process stream 32 may be maintained between a range of about 0.09: 1 to about 4:1. The equivalence ratio of the reactable process stream 32 may be maintained at or above the lower flammability limit for natural gas mixtures, i.e., above 0.4: 1, by virtue of the high local velocity of the process stream 32 (due to the constricted -flow through the mixing conduits 18) and the close proximity of the outlet of the mixing conduits 18 to the matrix bed 42.
  • the equivalence ratio in a FTO is maintained at about 0.35:1, which is well below the lower flammability limit for natural gas mixtures.
  • the equivalence ratio is maintained below the lower flammability limit in a FTO to prevent or reduce the risk of flashback in addition to other operational benefits.
  • flashback could potentially occur if the fuel-air mixture was maintained equal to or greater than its lower flammability limit. For that reason, in FTO's the fuel-air mixture is maintained at least about five percentage points below its lower flammability limit to prevent flashback.
  • Maintaining the fuel-air mixture at least about five percentage points below its lower flammability limit may facilitate excessive fuel consumption and overly conservative vessel sizing criteria. More particularly, less supplemental fuel is required to oxidize a process stream 32 having an equivalence ratio greater than the lower flammability limit (i.e., 0.4:1) because less dilution air is required to maintain a low equivalence ratio. Thus, the cost of fuel consumed by the FTO 140 is significantly lower than that of a FTO, which is directly attributable to the diptube assembly 10 of the FTO 140.
  • each mixing conduit 18 includes a series of apertures 30 for distributing the fuel stream 15 with the mixture 19 (containing air) at greater equivalence ratios than about 0.4: 1.
  • each mixing conduit 18 optionally includes two rows of four apertures 30. A detailed view of the top row of apertures 30 is shown in FIG. 6A. The top and bottom rows each optionally include four apertures positioned at 0°, 90°, 180°, and 270°, as shown in FIG. 6A. The adjacent apertures 30 are separated by 90° to promote uniform distribution of the fuel stream 15 within each mixing tube 18.
  • the apertures are positioned at 45°, 135°, 225°, and 315°.
  • the top row of apertures may be positioned at 0°, 90°, 180°, and 270°
  • the bottom row of apertures may be positioned at 45°, 135°, 225°, and 315°, respectively.
  • the adjacent apertures 30 of both the top and bottom rows are separated by ninety degrees with respect to each other, and the apertures of the top row are separated by 45 degrees from the nearest apertures 30 of the bottom row.
  • the mixing conduits 18 may incorporate any number of apertures 30.
  • the apertures 30 may be positioned at any angle with respect to each other to serve any specific purpose.
  • each aperture 30 is disposed through the wall of the mixing tube at an angle "A."
  • the angle "A” may be approximately 45°, for example.
  • the apertures 30 are positioned at angle "A" to direct the fuel stream 15 toward the outlet 22 of the mixing tube 18.
  • the diameter of the aperture 30 is inversely proportional to the velocity of the fuel stream within the mixing tube 18, i.e., the velocity of the fuel stream distributed through the aperture 30 increases as the diameter of the aperture decreases, and vice versa.
  • the diameter of each aperture 30 also impacts the required equivalence ratio and total heat input.
  • the aperture size may vary widely. By way of non-limiting example, the diameter of each aperture 30 may range from about 0.02 inches to about 0.25 inches.
  • the fuel stream 15 may be distributed through the inlet of each mixing conduit 18 and the mixture 19 may be distributed into the apertures 30 of each mixing conduit 18 to achieve a similar effect.
  • the supplementary fuel stream 15 may be directly distributed into the mixing conduits 18 through a series of injectors, tubes or conduits (not shown) to achieve a similar effect.
  • the fuel stream 15 may be distributed directly into the fuel plenum 16 and the fuel conduit 14 may be omitted.
  • the conduits 12, 14, and 18 are not limited to a circular cross-sectional shape, as other cross-sectional shapes are envisioned, such as square, rectangular, and so forth.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'invention concerne un ensemble tube plongeur pour un dispositif d'oxydation thermique sans flamme ayant un lit matriciel de milieu. L'ensemble tube plongeur comporte un conduit de combustible au moins partiellement positionné dans le lit matriciel pour distribuer du combustible. Un conduit d'agent oxydant est au moins partiellement positionné dans le lit matriciel pour distribuer des agents oxydants, le conduit d'agent oxydant étant séparé du conduit de combustible. Au moins un conduit de mélange est positionné dans le lit matriciel et configuré pour recevoir du combustible provenant du conduit de combustible et l'agent oxydant provenant du conduit d'agent oxydant. Le conduit de mélange est positionné pour distribuer la combinaison de combustible et d'agent oxydant dans le lit matriciel de milieu.
PCT/US2009/036724 2008-03-11 2009-03-11 Système et procédé d'oxydation thermique sans flamme à des rapports d'équivalence optimisés WO2009114571A2 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
US12/921,481 US20110283991A1 (en) 2008-03-11 2009-03-11 System and method for flameless thermal oxidation at optimized equivalance ratios
US14/298,019 US9970683B2 (en) 2008-03-11 2014-06-06 Apparatus and method for flameless thermal oxidation at optimized equivalence ratios
US15/947,988 US10234174B2 (en) 2008-03-11 2018-04-09 Apparatus and method for flameless thermal oxidation at optimized equivalence ratios

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US3558908P 2008-03-11 2008-03-11
US61/035,589 2008-03-11

Related Child Applications (2)

Application Number Title Priority Date Filing Date
US12/921,481 A-371-Of-International US20110283991A1 (en) 2008-03-11 2009-03-11 System and method for flameless thermal oxidation at optimized equivalance ratios
US14/298,019 Continuation-In-Part US9970683B2 (en) 2008-03-11 2014-06-06 Apparatus and method for flameless thermal oxidation at optimized equivalence ratios

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Publication Number Publication Date
WO2009114571A2 true WO2009114571A2 (fr) 2009-09-17
WO2009114571A3 WO2009114571A3 (fr) 2010-01-14

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US9970683B2 (en) 2008-03-11 2018-05-15 Linde Engineering North America Inc. Apparatus and method for flameless thermal oxidation at optimized equivalence ratios
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