TW200940155A - Flameless thermal oxidation apparatus and methods - Google Patents

Abstract

A thermal oxidizer is provided in which off-gases in a process stream are thermally oxidized within substantially the entire interior volume of an oxidation chamber. The thermal oxidation is conducted without the presence of a frame or with only a minor portion of one or more fuels being combusted in a flame.

Description

200940155 IX. INSTRUCTIONS OF THE INVENTION: TECHNICAL FIELD OF THE INVENTION The present invention generally relates to organic compounds in a thermal oxidation furnace for use in a oxidizing process stream, and more particularly to the use of flameless thermal oxidation. The apparatus and method of operating such a thermal oxidation furnace thereby decomposing organic compounds. [Prior Art] Ο

Thermal oxidation furnaces are typically used to oxidize one or more gases or vapors in a stream. This is done by subjecting the gases or vapors to elevated temperatures prior to being released into the atmosphere. The gas in the treatment stream is generally referred to as off-gas and generally contains volatile organic compounds (v〇c), semi-volatile organic compounds (svoc), and/or hazardous air pollutants (ΗΑρ) β. Process streams containing exhaust gases are typically by-products of industrial manufacturing or power generation processes. In a conventional thermal oxidizing furnace, the exhaust gas is oxidized by combining a treatment stream with a gas stream containing oxygen, and passing the combined gas stream through a flame or a combustion gas generated by, for example, a natural gas (four) material supply source. Carbon dioxide and water. In this way, the thermal oxidizer converts organic compounds that are unfavorable to environmental factors into harmless compounds that can be safely discharged to the atmosphere. The way in which the compound of the scorpion is thermally decomposed usually results in the generation of, for example, air pollutants such as C0 reaching the level of opposition of eight people. Ν0χ is due to the high temperature in the local area: CO is caused by complete combustion of the fuel during the combustion process in the thermal oxidation furnace. In order to reduce the degree of Ν0Χ and C0 generated during the thermal decomposition of the compound, it is known that a flameless oxidation process can be used in the thermal oxidation furnace. An example of such a process without oxidation is disclosed in U.S. Patent No. 5,1,65,884. In this patent document, a mixture of gas or vapor and air (and/or oxygen) flows into a bed matrix made of a strong heat resistant material, and the bed substrate has been preheated to spontaneous combustion of the mixture. Above temperature. This mixture begins to burn in the bed matrix and produces an exothermic reaction, forming a self-sustaining reaction wave in the bed matrix. This process is used to minimize enthalpy, C 〇 and other products due to incomplete combustion during the destruction of a particular gas or vapor in the process stream before the process stream is released to the atmosphere. Using this method, it is possible to obtain a degree of enthalpy of enthalpy of enthalpy (e.g., Ν〇2) of less than 〇 b 71b per million BTU, and the degree of co emission can be less than 1 〇 ppm. The bed substrate of the above-mentioned U.S. Patent No. 5,165,884 has the advantage that it can fix and stabilize the reaction wave during the combustion process. However, the bed substrate occupies most of the internal volume of the processing reactor, thus reducing the open volume available for processing the flow. The reduction in open volume in the reactor also reduces the residence time (residence) obtained under the conditions of the specified treatment stream and the specified reactor size, thus reducing the time available to destroy hazardous waste. The matrix produces a large pressure drop. This increases the operating cost of the process because the enthalpy of the process stream entering the process reactor is subject to increased (four) forces. When special materials from the process stream accumulate in the bed matrix When the bed base is degraded due to thermal shock (thermal Sh〇Ck), the pressure drop tends to increase with time. Finally, the increase in the force across the bed base may result in the need to change the bed material for 200940155. Therefore, there is a real need to develop a 埶4 diameter... oxidizing furnace capable of producing a very low degree of NOx and CO without causing the above-mentioned disadvantages from the above-mentioned defects. [Summary of the Invention] The method of forming a knife contained in a thermal fluid in an oxidation chamber. The jtb oxidation chamber has an inner liner capable of transferring sufficient heat to cause flow. The components in the stream are thermally oxidized. The method comprises the steps of initially heating the lining of the oxidation chamber and then, under some conditions, delivering the components to the oxidation chamber for heat transfer from the lining of the oxidation chamber. Initiating thermal oxidation of the components. The step of initially heating the oxidizing chamber liner comprises heating the liner to a preselected temperature sufficient to radiate or otherwise transfer thermal energy to initiate heat in the fluid stream. Oxidation. After the refractory lining is heated to a preselected temperature, it is possible that these components of one or more fuels are delivered to the oxidation chamber as a fluid stream. The conditions in the fluid stream are controlled such that The composition of the fluid φ stream produces flameless thermal oxidation by the effect of heat transfer from the refractory lining. Thus, the method of the method relies on thermal conduction from the refractory lining to initiate and sustain flameless thermal oxidation, thereby There is no need for a bed substrate, a preheated fuel stream and/or a combustion air stream, or a flue gas, as is required in conventional flameless oxidation processes. Steps. In one embodiment, one or more of the fuel components in the fluid stream are combusted such that the refractory lining can be initially heated to a preselected temperature. The fuel component of the fluid stream The overall concentration may be within the flammability range during the start mode. On the other hand, the overall concentration of the fuel component 7 200940155 exceeds the range of flammability, but the combustion air is present in the fluid stream by imaginary fuel components. Incomplete mixing produces an easy-to-dancing mixture, thus producing a diffused or partially pre-mixed flame. During the transition to the flameless thermal oxidation mode, for example by increasing the mixing of fuel and combustion air The local concentration of the component deviates from the range of susceptibility, and the flame of the material can be (iv) (4), whereby the anti-magic compound is burned in a flame in the burner. Other methods can be used to change the local concentration of the fuel component beyond the flammability range. Volatile organic compounds, semi-volatile organic compounds, and/or hazardous air pollutants may be present in the fluid stream as an additional component: while being oxidized during the innocent thermal oxidation process. These additional components are typically sourced from the process stream of an industrial manufacturing or power generation process and must be removed before the process stream is released to the atmosphere. The process stream can supply some or all of the combustion gases required for this process, or no combustion gases at all. If necessary, supplemental heat can be added to the oxidation chamber to compensate for heat loss due to the cooling effect of the enthalpy or fluid flow. This supplemental thermal energy can be continuously added, for example, by burning one or more fuels in another fluid stream in the oxidation chamber in a flamed manner. On the other hand, this supplementary heat is intermittently added, for example, by periodically operating the thermal oxidation furnace in the initial heating mode. When the process of the present invention is operated in a flameless oxidation mode, it is possible to achieve a degree of N〇x of less than 5 ppm (dry), less than 2 ppm (dry), and even less than 1 ppm (dry), and less than 1 ppm (dry) of c〇 degree. As used hereinafter, the extent of NOx and CO is expressed as a dry basis based on one millionth of each of 200940155. Even when supplemental heat energy is added to the oxidation chamber, a degree of enthalpy of between 1 and 12 ppm (dry) and a degree of CO of less than 1 ppm (dry) can be obtained. [Embodiment] Ο Referring now in detail to the drawings, first referring to Fig. 1, an embodiment of a thermal oxidizing furnace for performing flameless thermal oxidation of components in a fluid stream is indicated generally by the symbol 1 〇. The fluid flow is indicated by arrow 丨1 and is generally a gas or vapor stream that flows in a continuous or intermittent manner within the thermal oxidation furnace. The oxidizable component of fluid stream 11 can be in the form of a gas, a liquid, and/or a solid particulate. Examples of such ingredients include: fuels, waste products, and organic compounds. The organic compound includes volatile organic compounds, semi-volatile organic compounds, and/or harmful air pollutants. The thermal oxidation furnace 10 comprises a thermal oxidation chamber 12 having an outer casing 14 in which one or more layers of refractory linings are provided. These refractory linings are formed of any refractory material and have a high operating temperature. The physical and chemical properties required for other conditions present in the thermal oxidation chamber 12. The refractory lining 16 is castable, has plasticity, monuments, blankets, fibers, and other suitable forms, and generally contains ceramic materials. The material is made from oxidized sulphur, sulphur dioxide or oxidized town. Conformation is made by a combination of substances. The refractory lining 16 may also be formed of other materials such as refractory metal, a suitable refractory material and an alloy of these metals, and a refractory lining, followed by a lower thermal conductivity lining. The heat loss generated by the outer casing 14 is further reduced. 9 200940155 In the inner region of the inner casing 14 of the liner, an open: inner body #18 is defined, and the flameless thermal oxidation occurs in this inner volume, which will be described later. The size of this open internal volume is created such that U flows the fluid to achieve the desired residence time, and this fluid flow is directed to the particular treatment performed = flowing through the thermal oxidation chamber 12 in accordance with the desired volumetric flow rate. Under normal conditions, the residence time can be selected such that for oxidizable components in the process stream, complete combustion and/or desired damage removal efficiency can be obtained. Preferably, the housing 14 is cylindrical and oriented in a horizontal orientation, but may also have a cross-section of a polygonal or other configuration' and/or it may be oriented vertically or at an intermediate angle. The housing 14 has an at least partially open upstream end 20' and a downstream end that is at least partially open & using the terms "upstream" and "downstream" for fluid flow during operation relative to the thermal oxidation furnace 11 passes through the desired direction of the flow of the oxidation furnace 12. The thermal oxidation furnace K) additionally includes a burner 24 connected to the upstream end 2 of the thermal oxidation chamber 12 by a selective transition zone 26. The downstream end 22 of the thermal oxidation chamber 12 is connected to the exhaust gas f 30 by a similar selective transition zone. Through this exhaust pipe, the reaction product produced by the thermal oxidation process can be released to the atmosphere. On the other hand, the helium oxygen, the swim end can be in fluid communication with the downstream device 31, which may benefit from the low NOx, low CG, high temperature fluid flow of the class q; examples of the swim device 3i include but are not limited For processing heaters, boilers, (eg, ethylene cracking unit, hydrogen reformer, etc.), air heaters, dryers, gas full wheels, and heat exchangers. Therefore, the thermal oxidation furnace 1 can be used by 200940155 to provide a hot flue gas stream with a low degree of NOx and c〇, thereby replacing a part of the conventional method for igniting downstream equipment. The burner 24 is a blast burner capable of generating a strong whirlwind ' thereby ensuring thorough premixing of the combustion air with the fuel gas. Preferably, the fuel of the burner 24 is a gas, generally natural gas or refined fuel gas, but other fuel gases such as hydrogen, methane, ethane, propane, butane, or other hydrocarbons may also be used, Carbon monoxide, and various mixtures thereof. Various additives and diluents (e.g., nitrogen, carbon dioxide, and/or water vapor) may also be added to or present in the gas. Some or all of the fuel may be in the form of liquid or solid particulates. Other types of burners can also be used, such as induction vented burners, natural vented burners, premixed burners, and partially premixed burners. As can be seen from Figure 2, in the embodiment shown, the burners 24 are packaged in three. The p-body 32 is provided with one or more layers of the refractory lining 34 of the above type. It is also possible to arrange the layer insulating lining % between the hot surface refractory inner portion and the inner surface of the outer casing 32. Preferably, the housing 32 is cylindrical and may have a polygonal or other configuration. The <1 U has a side wall 36 and an opposite upstream end 38 and downstream end 4''. The inner casing 32 defines an open interior anterior chamber (sand _) 42 that is in fluid communication with the oxidizing chamber 12 located downstream of the combustor 24. An obstructing valve 44 made of a fossil material may be located at the downstream end 4 of the combustor casing n to produce a reduced passage 45 from the front chamber 42 to the downstream oxidation chamber 12. The blocking valve 44 may have a moment "11 200940155 face" as shown in the figure or it may also be formed by an inwardly directed inlet end and an outlet end to form a more hydrodynamic structure. In some applications, The occlusion valve 44 » / - nozzle assembly 46 is positioned at the upstream end 38 of the combustor casing 32 to deliver a combustible mixture of fuel and air to the anterior chamber 42. In one embodiment, the nozzle Assembly 46 includes an elongated and centrally located fuel gun 48' from a fuel source 5 () that supplies fuel to the fuel rush through conduit 52. A suitable flow regulator 54 adjusts the volumetric flow rate into the fuel rush. 48 terminates in a fuel tip piece %. The fuel tip member has a plurality of fine holes (not shown) through which the fuel flow indicated by the arrow 'arrows is discharged into the front chamber 42. The fuel grab 48 can be in the axial direction

The upward movement causes the positioning of the fuel tip member 56 to be changed relative to a surrounding throat structure 58 having a region of reduced profile, as will be explained in more detail later. Alternatively, the second fuel tip member in combination with the fuel grab 48 or another fuel gun (not shown) may be spaced from the first fuel tip member 56 such that the fuel may be opposite the throat structure 58. And injection at different locations. * The fuel grab 48 is surrounded by a can 59 in which a plurality of rotating blades 60 are positioned in an annular opening extending around the can 59. The rotary vane 60 is mounted to the spaced apart ring members 03a and 03b which are fixed to the canister 59 near the annular opening. The ring member 63a closest to the fuel tip member 56 has an inner diameter that is substantially equal to the inner portion of the can 59 so that it does not block the flow of fluid within the can 59 toward the fuel tip member 56. The oxy-combustion air stream or other oxidant system 12 200940155 shown by arrow 61 flows into the canister 59 through the rotating blades 60 and then flows into the front chamber 42. The rotating blades 60 can cause a strong rotational motion of the combustion air flow, thereby assisting in the mixing of the combustion air with the fuel flow discharged from the fuel tip member 56. Combustion air is supplied from a source of combustion air 64 to the canister 59 via a conduit 62 and the volumetric flow rate is adjusted by a flow regulator 65. The desired mixing of the fuel stream 57 with the combustion air stream 61 can be performed using other mechanisms. As an example of such a mechanism, the combustion air stream 61 can be delivered to the canister 59 through one or more angular discharge nozzles that can cause the combustion air to rotate. It is to be understood that it is not necessary to cause the fuel stream 57 or the combustion air stream 61 to rotate as long as sufficient turbulence is generated to cause the fuel stream 57 to be deeply mixed with the combustion air stream 61. Combustion air stream 61 and/or fuel stream 57 may be supplied to combustor 24 at ambient temperature. On the other hand, the combustion air stream 61 and/or the fuel stream 57

It may be preheated by a heat exchanger 66 where the heat exchanger & I 疋 is supplied by the combustion process produced in the thermal oxidation furnace 10 or from a suitable heat source. Preferably, combustion air stream 61 and fuel stream 57 are supplied to combustor 24 at a sufficient pressure to force fluid stream u to flow forward through oxidation chamber 12' without recirculation. The supply stream 64 of the combustion air stream 61 may contain some or all of the process stream 68 containing water products, organic compounds (including: volatile organic compounds and semi-volatile organic compounds, and/or harmful air pollution =) . Examples of such compounds and contaminants include hydrocarbons, sulfonation, chlorinated solvents, halogenated hydrocarbon liquids, dioxin, and polygas 13 200940155 bis biphenyl: thus 'treatment stream 68 can be - waste gas or industrial manufacturing or power generation A by-product of the process. The supply source 64 that ignites the flow of air based on the characteristics of the process stream 68 and the oxygen content may also contain atmospheric or some additional source of oxygen. Additionally, one or more portions (or even all) of the process stream 68 may = bypass the space 59' having combustion air and may be delivered to the front chamber 42 and/or the oxidation chamber 12 at one or more downstream locations, such as by Injections of 〇7〇, η and/or ~ can change the number and location of injections of itch 70, 71'72 to suit a particular application. Flow regulators 73a through 73c are provided for regulating the flow rates of different portions of the secondary stream 68. The different fuels, combustion air, and process streams 57, 61 and : volumetric flow rates are monitored and adjusted using appropriate process controllers. The process controller 74 can adjust the flow rate by automatically controlling one or more flow regulators 54, 65 and ^ to 73c. Alternatively, one or more flow regulators $ to 73c can be manually adjusted. 』 / 3a = structure 58 is positioned at the upstream end % of the anterior chamber 42, and, a: the embodiment includes a ring (four)%, the annular wall is positioned from the throat white 58 with the reduced profile area # Shrink or gradually sharpen. This throat structure 58 is passed through the rotating blade 60 structure 58 by the combustion air stream 6 discharged from the crucible 6 turns. The meat 4 of the throat 78 passes through the inner diameter of the throat member 63b before entering 42 to substantially equal to the ring in which the rotating blade 60 is mounted. During the start mode, it is positioned below the centerline of the throat 78: the fuel tip member 56, such that The fuel stream 57 is discharged, and the fuel tip member % at the first position at the combustion air = 61 is discharged from the rotating blades 6 〇 14 2009 40155 at the second position. The second position is located at the fuel stream 57. A preselected distance upstream of the first discharge location causes the two streams to first mix at the throat 78 or downstream thereof. Positioning the fuel tip 50 downstream of the throat 78 under pre-selected combustion air to fuel ratio limits the complete mixing of fuel and combustion air and allows local fuel concentrations to be within flammability In this way, the fuel can be burnt in the chamber 42 in a flamed manner. Depending on the flow conditions, the flame mk extends to the upstream portion of the oxidation chamber 12 from the next month to 42. When the ?-burning beta gas flows through the oxidation chamber 12, the fire resistant liner 16 of the oxidation chamber 12 is heated to a preselected temperature whereby the fuel and air mixture flowing through the oxidation chamber 12 can continue. Flameless thermal oxidation. When natural gas is used as the fuel source, the method of the present invention has proven successful in operating in a preselected temperature range (approximately 1900 to 2400 〇F). By further optimizing the apparatus and method, it is believed that this pre-selected temperature can be expanded from about 1700 °F to about 30004. © After the refractory lining 16 reaches a pre-selected temperature, the process flow switches from the start mode to the flameless thermal oxidation mode, in which the components of the fluid stream u delivered to the oxidation chamber 12 are oxidized. Different methods can be used to extinguish the flame in the pawl/claw 1 1 during the transition phase from the start mode to the 2 oxidation mode. In the embodiment shown, switching from the start mode to the h-free thermal oxidation mode can be achieved by moving the fuel tip member % upstream of the throat. Movement of the fuel tip member 56 enables the fuel stream 57 to be discharged from the fuel tip member 56 in the second position such that fuel exiting the fuel tip member 56 impinges on the throat of the burner. Thus, 15 200940155 fuel stream 57 and rotating combustion air stream 61 contact each other at a location upstream of throat 78 to allow for a more complete mixing of fuel stream 57 with combustion air stream 6 i before the mixture passes through throat 78. . Due to the more complete mixing of the fuel with the combustion air stream 57, the air to fuel ratio will be below the lower limit of flammability throughout the mixture and extinguish the visible flames of months J to 42. As another method, the fuel delivered via injection 埠 can be used in the start mode. In this embodiment, the fuel tip member 56 is secured to a location upstream of the throat 78, and after reaching a preselected temperature, a fuel valve (not shown) switches the fuel from the injection port to the fuel. Tip member 56. In either case, the fuel and combustion air mixture continues to be thermally oxidized due to the heat transferred by the refractory lining 16 within the oxidation chamber 12, while there is no flame in the oxidation chamber 12. Moreover, there is no need for steps such as requiring recirculation of flue gas as in prior art processes, preheating fuel, combustion air 'and/or process stream 57, 61 or 68, and/or using a bed substrate within oxidation chamber 12. After extinguishing the visible flame, the degree of NOx in the flue gas drops rapidly, including less than 5 ppm (dry), less than 2 Ppm (dry), and even less than 1 ppm (dry), and does not increase CO degree. When stage combustion is not used, a degree of enthalpy of less than 2 ppm (dry) and a degree of CO of less than 1 ppm (dry) can be consistently achieved at operating temperatures up to 2380 °F. Even with a staged combustion of 14.4% fuel in a flamed manner, at the operating temperature of i99〇〇f, a degree of NOx between 6 and 12 ppm (dry) and a degree of CO less than 1 ppm (dry) can be achieved. The thermal oxidation of fuel and other components in fluid stream 11 releases thermal energy' and then continues to heat the fire lining 16. According to the special treatment strip 16 200940155: The heat released can extend the processing flow in the Yingyan 敎 oxidation mode. You can know that the hot rolling can be used to increase the fuel by other methods. The flow 57 is combined with the combustion (four) and the m part, thereby achieving the switch from the start mode to the fanless oxygen easy to record, as described previously, except that an axial movement, a work such as, for example, a mobile fuel grab is used. In addition, -p is used to axially pass from the first fuel tip member 56, causing the fuel stream 57 to be at a position to be discharged from the axial position. At the beginning of the circumstance, the stream 57 is thoroughly mixed with the fuel stream 61 through the fuel tip 2 = Γ = stream 57 closest to the throat structure 58. Drinking the ',, and route to another fuel's fuel stream 57 and fuel air stream two during the flameless thermal oxidation mode: more complete mixing. In addition to increasing the flow of fuel 57 and the flow of combustion air 6 ', the transition from the start mode to the flameless thermal oxidation mode can be varied by varying the relative flow rate of fuel flow 57 relative to combustion air flow 61. Change the proportion of local combustion air to fuel. In the start mode, the ratio of combustion air to fuel is within the flammability range. In order to transition to the flameless thermal oxidation mode, the ratio of combustion air to fuel can be adjusted such that the local ratio is sufficiently outside the flammability range to allow for the visible flame used during the mode. 17 200940155 Exceeding the current flame speed is a common method used to extinguish the visible flame during the transition to the flameless thermal oxidation mode. In the start mode, the flow ratio of fuel flow 57 to combustion air flow 61 is maintained below the upper limit of the flow rate. In the flameless oxidation mode (4) 'increasing the flow rate of the fuel stream 57 and the combustion air stream 61 - or both, causing the mixture to flow at a grip speed greater than the turbulent flame speed, thereby extinguishing the flame, and due to the refractory lining" The reason for heat conduction is to cause thermal oxidation of the fuel in the oxidation chamber 12 with the combustion air mixture. As another example, in addition to increasing the velocity of the fuel and combustion air mixture = flow rate above the turbulent intensity, it is blameless. The speed of the flame reaches a speed below the mixture of fuel and combustion air. This point can be achieved in many ways. For example, the internal flow geometry of the burner Μ can be changed, for example, from the start mode to the flameless thermal oxidation mode. During the transition period, by moving the position of the injected fuel by the previously mentioned method, as another example, a flame holding structure (not shown) can be placed in the front to 42 to fix the flame during the start mode. Then, the flame holding structure can be moved or changed to reduce the velocity of the stream during the transition to the flameless oxidation mode, resulting in It no longer settles the flame. This process can be cycled between the start mode and the flameless oxidation mode using pre-selected intervals, for example, where the refractory lining 16 cools below the continuous fluid flow η. In the case of temperatures required for the thermal oxidation of the flame, additional heat energy is required during oxidation t 12. This cooling may occur as a result of passing through the outer casing 14 of the oxidation chamber 12, or fuel, combustion air, and/or process streams 57, 61. Heat loss due to cooling effect with 68. Flameless 18 200940155 Thermal oxidation can last for a period of time, such as one hour or longer (including indefinite periods), depending on the specific process flow and equipment conditions used. In other applications, as described above, it may be desirable to add supplemental heat to the oxidation chamber 12 to compensate for the passage of the outer casing 14 with fuel, combustion

The heat deduction caused by the cooling effect of gas or (4) 57, 61 Xiao 68 and its towel. These fuel, combustion air, and/or process streams 57, 61 and 68 are delivered to the burner μ or oxidation chamber 12 at a temperature below that at which flameless oxidation occurs. For example, 'the fuel, combustion air, and/or process stream may be preheated continuously or intermittently; the supplemental fuel may be passed through a plurality of injection ports (eg, injection port 71 with or without a portion of process stream 68, and/or injection 槔) 72) introduced into the oxidation chamber 12; by burning the supplemental fuel in a flame mode; by using a resistive twist, a knife heat/thickness, and/or operating the burner 24' in an initial heating mode Add supplemental heat. By adding this supplemental heat by burning the fuel in a flame-like manner, the degree of enthalpy and c〇 can be increased, but the overall degree is still significantly lower than that of the fourth embodiment of continuing to burn all of the fuel to operate the thermal oxidizer 10. degree. During operation of the thermal oxidizer 1G in the flameless oxidation mode, a mixture of the reactants and the combustion air stream 57 and the selectively treated stream 68 are delivered to the oxidation chamber 12 as a premixed mixture. Its combustion air to fuel ratio is based on the desired operating conditions in the particular application scenario being implemented. The thermal oxidation process continues for a desired period of time due to the thermal oxidation of the fuel and other components of the fluid stream to a desired ratio of combustion air to fuel and the individual flow rates of the combustion air stream and fuel are substantially adjusted (4) (4) supply is sufficient The ability to perform. In addition, the local combustion air to fuel ratio or the flow in the flow stream u should be lower than the specific fuel or fuel mixture used.

The lower limit of flammability, or the flow rate of one or more of the fluid stream n, the combustion air stream 61', and the fuel stream 57 is adjusted such that the flow rate of the fluid stream is greater than the fuel and other combustible components in the fluid stream 11. Turbulent flame speed. For example, when natural gas containing about 95% methane is used as a fuel, the ratio of combustion air to fuel is about 2 〇 : 1 or more. As long as the combustion air and fuel concentration are outside the flammability range of the mixing temperature of the front chamber 42 (four), and the fluid flow through the yttrium oxide 12 (four) fluid is thoroughly pre-mixed, the thermal oxidation generated in the oxidation to 12 will be flameless. of. Excess air and/or diluent, such as nitrogen, carbon dioxide, and/or water vapor, can be injected into the anterior chamber 42 to lower the fuel concentration and thereby remain below the lower flammability limit to reduce access to the anterior chamber 42. Unnecessary flashback phenomenon

If present, by increasing the velocity of the fluid stream 11 flowing from the front chamber 42 into the oxidation chamber 12, and shielding the front chamber 42 from the radiation emitted by the oxidation chamber 12, the internal blocking valve 44 may additionally reduce the chance of flashback. . The presence of a diluent enhances fuel efficiency because the flameless process can operate at a lower oxygen content of the combustion air streamer. The composition of the fluid stream 11 that is thermally oxidized in the above-mentioned no process can be: a compound that can withstand thermal oxidation, such as: fuel, waste materials, machined materials (including volatile organic compounds and semi-volatile organic chemical burns) Second, there are: air pollutants. In which the thermal oxidation furnace 10 is only used as a Lai

In the case of operation of the vessel, _ Μ 4 e U or more fuels may be fluid stream u: to thermally oxidized components. In other words, the present invention encompasses the process in which the furnace 10 does not remove contaminants from the process stream, but does so as to prevent hot smoke from the burners of the <20200940155> The gas acts as other uses in, for example, the downstream device 31.

The burner 24 provides a convenient mechanism for preheating the oxidation furnace 12 and then premixing the fuel and combustion gases prior to delivery to the oxidation chamber 12. However, it is to be understood that the oxidation of t 12 can be preheated by other heat sources other than the burner 24. In addition, the fuel and combustion air may be premixed by other mechanisms after the fuel and combustion air enter oxidation to 12. Thus, the present invention encompasses a process that does not require the use of burner 24 and otherwise supplies thermal energy, or includes where burner 24 is an induction ventilator, a natural ventilator, or a partially premixed burner. The treatment of the present invention does not require the use of such a bed substrate as used in U.S. Patent No. 5,165,884. Therefore, substantially all of the internal volume in the oxidation chamber 12 can be used as the flow of the fluid stream 11 subjected to the flameless thermal oxidation. Therefore, in the method of the present invention, the disadvantages mentioned above with respect to the bed substrate can be avoided, but still a very low degree of N〇x and C〇 can be achieved. Although a bed substrate is not required in the flameless thermal oxidation process of the present invention, it may be desirable in some applications to include a vertical body or other mixing device within the oxidation chamber 12 to promote mixing of the fluid stream u and / or fixed flame, to supply supplemental heat. It is also possible to use __ vertical bodies or other mixing devices as the flame holding structure in the front chamber 42. As previously mentioned, changing or moving the flame maintaining structure may change the velocity of the fuel in the fluid stream U to promote combustion of the fuel in a flamed manner to initially heat or reheat the oxidation chamber to the fire. The mode, as well as the transition between modes 21 200940155, which thermally oxidize the fuel in a flameless manner by heat conduction from the refractory lining 16 is performed. The flue gas reaction product leaving the oxidation to 12 can be sent to the exhaust pipe 3 to be discharged to the atmosphere, and the flue gas can also be used as a heat exchange medium to preheat one of the fluid streams u before being transported to oxidation to 12. Multiple ingredients. In addition, hot flue gas can be used in downstream equipment such as treatment heaters, boilers, reactors (e.g., ethylene cracking units, hydrogen reformers, etc.). The following examples are provided for illustrative purposes only and are not intended to limit the scope of the invention. 〇 Example 1 At room temperature, combustion air having an air form is delivered through a rotating blade 6〇 at a flow rate of 1140 〇〇scf/hr. In the front chamber 42, a fuel having a natural gas form at room temperature is injected into the front chamber 42 through the fuel tip member 56 at a flow rate of 555 〇scf/hr. Ignite and combust the fuel and combustion of the air oxides ' until the oxidation chamber 12 reaches 188 Torr. ? The temperature is up. Once the oxidation chamber 12 is preheated in this manner, the fuel tip member 56 is pulled back about 3.5 inches from the centerline of the burner throat 78 such that the mixture of fuel helium and combustion air passes through the burner throat 78. A more complete mixing is produced, so the flame of the burner can be extinguished. The flow rate of fuel and combustion air is maintained to be almost unchanged, and a premixed flow of fuel and combustion air passes through the burner throat 78 into the front chamber 42 without visible flames, and because of the flame-burning fuel The resulting burning roar ceases to exist. Due to the heat transfer of the preheated refractory lining 16 in the oxidation chamber 12, the fuel continues to oxidize in a stable, flameless oxidation process 22 • 200940155 . The flameless oxidation process is substantially in equilibrium and the degree of NOx is measured to be less than ippm (dry) and the degree of CO is less than 1 ppm (dry). The process lasts for 8.5 hours and causes heat loss through the outer casing 14 of the oxidation chamber 12 and the cooling effect of the fuel and combustion air delivered to the burner 24 at room temperature, such that the burner 24 is downstream When the temperature in the oxidation chamber 12 is cooled to a temperature of 1500 cF, it is stopped. When this process is stopped, the exit temperature of the oxidation chamber 12 is still i88 〇〇F. Example 2 重复 Repeat the test of Example 1 with the following changes in parameters. (丨) the combustion air flow rate is reduced to 100200 scf/hr, and (2) the fuel flow rate through the front chamber 42 is reduced by burning the fuel in sections. The total fuel flow rate is 550 〇 SCf/hr, and after splitting, 85 • 6% of the fuel is premixed with all of the combustion air prior to injection into the front chamber 42 such that the remaining 14% of the fuel is injected through the two fuel tip pieces π in the oxidation chamber 12 downstream of the combustor 24. The fuel injected into the oxidation chamber 12 through the fuel gas tip member is φ in a flame-like manner and directly heats the refractory lining 16 to stabilize the flameless oxidation process in the oxidation chamber 12. The outlet temperature of the oxidation chamber 12 is 1990 °F due to the increase in heat input. Since a part of the fuel is burned in a flamed manner, the degree of NOx increases and changes from the outer jaw to 12 ppm (dry). The CO level is still below 1 ppm (dry). This test is intended to end in 44_5 operating hours, so it seems that this process is self-sustaining. The following test shows that the gas tip member downstream of the burner 24 is supplied in stages, not exceeding the flammability limit in the front chamber 42, which can reach even about 2000 °F, 2100. Higher operating temperatures of °F, 2200°F, 2300〇F and 2400 F. By the ability to intimately mix the fluid stream 11 with the fuel supplied to the stage oxidized to 12, a degree of enthalpy and c〇 below ippm can be obtained even at about 2000 F'. I believe that higher temperatures can also be achieved. Example 3 The test conditions of Example 3 demonstrate an example in which the turbulent flame speed is exceeded before the refractory lining 16 is sufficiently preheated, thereby rendering the flameless operation flammable to the air/fuel mixture in the anterior chamber 42. Lower limit. The combustion 〇 air flow rate was 245,640 scf/hr, the natural gas flow rate was 18,357 scf/hr, and the enthalpy oxidation furnace operating temperature was 238 pF. The combustion air and natural gas are premixed in the front chamber 42 to produce 5.87% by volume of the premixed fuel component, which is the lower flammability limit (5% by volume) above the ambient temperature. The oxidation process does not flash back into the front chamber 42 and represents a turbulent flame velocity that passes through the reduced diameter passage 45. The enthalpy concentration for this process was 1.3 ppm (dry) and the CO emissions were too low to measure (less than 1 ppm (dry)).范例 Example 4 By combining 2002scf/lir of C02 and 62280scf/hr of fresh air to produce 14.5% by volume of oxygen, a mixture of low-oxygen combustion air is produced, which is sent through the rotating blades 60. Inside the chamber 42. A fuel having the form of natural gas at room temperature is injected into the front chamber 42 through the fuel tip member 56 at a flow rate of 5475 scf/hr. The fuel and low oxy-combustion air are mixed in the front chamber 42 and enter the thermal oxidation chamber 12 to be oxidized in a flameless manner. Since the content of oxygen in the generated flue gas is 2% by volume (dry), the concentration of c〇 is too low to be measured, the concentration of antimony in the flue gas is i 2 ppm (dry), and the operating temperature is (9) 1 °F. This test example shows that the thermal oxidation furnace can be operated by a low oxygen combustion 2 gas stream, a flue gas recycle stream, and/or a low heating value waste stream. The results of this test also show that the flameless treatment can operate at a lower oxygen content in the combustion air than in a conventional burner with a flame form. Thermal efficiency can be obtained when using a low oxygen content combustion air source because only a small amount of fresh air needs to be added to this low oxygen content stream to maintain stability. Typically, conventional burners require more than 18% by volume of oxygen in the combustion air at room temperature to produce helium operation, but this test exhibits a steady state by burning 14-5% by volume of oxygen in the air. operating. From the above description, it is apparent that the present invention can still achieve all of the above objects and the advantages of the structure itself by adjustment and change. It will be appreciated that some features and combinations may be utilized and the invention may be practiced without other features and combinations. This is conceivable within the scope of the invention. Many other possible embodiments are possible without departing from the scope of the invention. It is to be understood that all of the present invention and the drawings are described as illustrative and not limiting. BRIEF DESCRIPTION OF THE DRAWINGS The following drawings form part of the description of the present invention, and reference is made to the drawings and 25 200940155 for a more detailed description of the present invention. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is a view showing a portion of a thermal oxidation furnace according to an embodiment of the present invention to show the combustion portion of the thermal oxidation furnace of Fig. 2 for schematically showing the thermal oxidation furnace. [Main component symbol description] 10 Thermal oxidation furnace 11 Fluid flow 12 Thermal oxidation chamber U Housing 16 Refractory lining 17 Small thermal conductivity 18 Open internal volume 20 Upstream end 22 Downstream end 24 Burner 26 Transition zone 28 Transition zone 30 Exhaust pipe 31 Downstream equipment 32 Enclosure 34 Refractory lining 35 The insulation is lined with some parts. Ο 〇26 200940155 Side wall downstream end downstream end front chamber blocked valve channel 〇 nozzle assembly fuel gun fuel source conduit flow regulator fuel tip fuel flow throat structure tank rotating blade air flow conduit ring ring supply source flow regulator heat exchange Processing stream 27 200940155

70 Injection 埠 71 Injection 埠 72 Injection 埠 73a Flow 々 /r Instant 73b Flow Adjuster 73c Flow Adjuster 74 Process Control 76 Ring Wall 78 Throat

28

Claims (1)

, 200940155 X. Patent application scope: i. A method for thermally oxidizing a component in an oxidation chamber, the oxidation chamber having an inner liner, the method comprising the steps of: initially heating the lining of the oxidation chamber; and then at some Under conditions, the component is delivered to the oxidation chamber, which is oxidized by heat transfer from the heated oxidation chamber liner. . The method of claim 1, wherein the step of transporting the components into the oxidation chamber comprises oxidizing the components in a fluid stream.琢3. The method of claim 2, wherein the method comprises the steps of: flowing the fluid stream through the oxidation chamber during or after thermal oxidation of the components/4, as in the method of claim 3 Included in the steps of: providing one or more fuels between the components in the fluid stream, and maintaining conditions within the oxidation chamber such that the fluid is passed through the heat transfer from the oxidizing chamber; One or more fuels within the stream produce a thermally oxidized hit body stream through the oxidation chamber. 1 a step of oxidizing a chamber to cause thermal oxidation of one or more fuels within the fluid stream to include providing one or more fuels within the fluid stream at a local concentration below the lower flammability limit, The fluid stream passes through the oxidation chamber. 6. The method of claim 5, comprising the step of reheating the oxidation chamber (4) by changing the conditions in the oxidation chamber, the one or more fuels in the fluid stream being combusted. 29 200940155 7. The method of claim 6, wherein the conditional step comprises changing the chemical conversion of the one or more fuels: it is above the lower limit of flammability. P / Farming' makes 8. For example, in the method of applying for patent scope 帛 4, * * species ά ~, T maintains the oxidation chamber I::: one or more fuels to produce thermal oxidation step ^ The packet 3 is caused to flow through a reduced diameter passage at a firing rate greater than the one or more fuels.疋Xμ 9. The method of claim 8, comprising the steps of: reheating the oxidation chamber by changing conditions in the oxidation chamber. One or more fuels in the fluid stream produce combustion. The method of claim 9, wherein the step of varying the conditions in the oxidation chamber comprises varying the flow rate of the fluid stream below a turbulent flame velocity of the one or more fuels. The method of claim </ RTI> </ RTI> wherein the step of initially heating the oxidized to the inner liner comprises, under conditions, transferring the components to the chemical chamber to cause combustion of the components. ❹ 12. The method of claim 2, wherein the step of initially lining the interior lining comprises transferring the components to the oxidation chamber by a fluid stream. # # 13. The method of claim 1, wherein the step of initially heating the emulsified chamber liner comprises providing one or more fuels in the components of the fluid stream. 14. The method of claim 1, wherein the method comprises the steps of: flowing one or more fluids through the 30 '200940155 chamber to make the fuel or fuels Producing the initial heating of the lining; and then changing the strips: causing the oxidizing chamber to produce the composition due to the heat transfer of the oxidizing chamber lining. 15. The method of claim 14 is as follows: "To the oxidation chamber" includes the transport of the components. The delivery of 3 has - or a plurality of fuels 16. As claimed in the patent specification: changing the conditions, heating the oxidizing chamber lining. In accordance with the method of item 15, the one or more fuels are additionally contained in the following step of combustion and re-circulated as in the patented range of steps of thermally oxidizing shai and other components. The method of item 16, comprising the steps of: and reheating the lining of the oxidizing chamber, such as the method of the fourth item, wherein the step of changing the cattle comprises the one or more fuels Change the local concentration within the flammability range beyond the flammability range.方法 Μ. The method of claim 18, wherein the method comprises the steps of: mixing the one or more fuels in the fluid stream to produce a change in the flammability range of the one or more fuels. The concentration is outside the range of flammability. 20. The method of claim 14, wherein the step of changing the conditions comprises changing the flow rate of the fluid stream from below the turbulent flame speed to above Turbulent flame velocity of one or more fuels. 21. The method of claim 4 of the claim 5 includes the following steps: including volatile organic compounds, semi-volatile organic compounds, and/or hazardous air 31 200940155 π dyes as the clock towel ingredient. 22. The method of claim 21, comprising the step of adding a volatile organic compound, a semi-volatile organic compound, and/or a hazardous air/loss material from a treatment stream to the fluid stream. 23. The method of claim 22, comprising the step of adding at least a portion of the process stream to the fluid stream at a location within the oxidation chamber. 24. The method of claim 22, comprising the step of: adding at least a portion of the treatment stream to the fluid stream after transporting the fluid stream to the oxidized to the side of the host . 25. The method of claim 5, comprising the step of premixing at least a portion of the one or more fuels with combustion air in the fluid stream prior to delivering the fluid stream to the oxidation chamber. 26. The method of claim 25, comprising the step of introducing another fuel stream containing - or a plurality of fuels into the oxidation chamber, and wherein - or more of the fuel in the another fluid stream The oxidation chamber is burned to add supplemental heat to the oxidation chamber. 27. The method of applying for patent scope No. 1, τ 祀 乐 , includes the following steps: maintaining the thermal oxidation for more than one hour. 28. The method of claim 4, wherein the step of providing one or more ancestors in the component of the fluid stream comprises the steps of: removing natural gas, refining fuel gas, and hydrogen methane. , ethane, propane, butane 'other A fuel is selected from one or more of the group consisting of hydrocarbons, carbon monoxide, and mixtures thereof. 32,200940155 A method of claim 28, comprising the step of adding one or more diluents to the fluid stream. 3. The method of claim 4, wherein the step of providing one or more fuels between the components in the fluid stream comprises including the natural gas package 3 as the one or more fuels. One of the fuels. Ο ❹ 31. The method of claim 3, comprising the step of pre-pulsing the fluid stream before flowing the fluid through the oxidation chamber. The method of claim 4, wherein the step of initially heating comprises heating the oxidized inner lining to a temperature range between 1800 and 3000 oF. The method of claim 32, wherein the step of providing one or more /, :: comprises the inclusion of natural gas in the components of the fuel stream. The method of claim 3, wherein the method of heating the first: = snail comprises: generating a hot flue gas by combusting a fluid that is in fluid communication with the oxidizing chamber; The hot flue gas is then heated to heat the liner to a preselected temperature. 35. The method of heating the oxidation chamber according to the application of the patent application No. 34, the method of heating the chamber includes the following steps: during the first stage of the fuel, the one or more air or other oxygen is burned. # ] The burner - in the inner chamber 'and introduces the second position in the second position into the interior chamber, the upstream portion of the Μ ' position - a predetermined distance. The method of claim 35, comprising the step of: or making a more complete mixing of the plurality of fuels with the combustion air, thereby causing the components to thermally oxidize within the oxidation chamber. 37. The method of claim 2, & includes the following steps: preventing recirculation of the fluid stream. 38. A method for thermally oxidizing a component of a fluid stream in an oxidation chamber, the fluid stream comprising one or more fuels, the oxidation chamber having an interior and lining the fire. The method comprises the steps of: Providing a fluid stream containing a thermally oxidizable compound comprising a &lt;multiple fuel and combustion air; (b) heating the refractory lining of the oxidation chamber to a preselected &amp;degree; and (c) Under conditions, the fluid stream is passed through the oxidation chamber, causing the composition to be thermally oxidized due to the heat transfer of the refractory lining, and the fluid stream needs to be recycled. 39_ The method of claim 38, which includes the following steps: Repeat steps (b) and (c) in your order. 40. The method of claim 38, comprising the step of providing a fluid stream comprising providing a fluid containing methane and combustion air. 41. The method of claim 38, wherein the step of heating the oxyhydrazine to the refractory lining comprises burning one or more fuels in a combustor in communication with the oxidizing chamber A hot flue gas is generated and the flue gas is delivered to the oxidation chamber, thereby heating the liner to pre-select the temperature of the woman. 42. The method of claim 41, comprising the steps of: β 34 , 200940155 heating the lining in the oxidation chamber, such as 咕* 呵 — - a fuel introduced to the burner at a first location The inner „ ^ 丨谷至中, and the combustion air is introduced into the inner chamber in the second position, the first position is located at a predetermined distance upstream of the first position. w 43. The method of the invention comprises the steps of: making the one or more fuels more completely mixed with the combustion air to stop the combustion of the one or more fuels in the burner, and (iv) by the oxygen: The heat conduction of the fire lining allows the fuel to be oxidized. The method of claim 41, wherein, under some conditions, the fluid stream is passed through the oxidation chamber to cause thermal oxidation of the components. Step 2 'contains that the local concentration of one or more fuels in the fluid stream exceeds the flammability range of the one or more fuels. 45. The method of claim 44, comprising the steps of: Varying the local concentration of one or more fuels in the fluid stream to lie within the flammability range of the one or more fuels, thereby combusting the one or more fuels' thereby reheating the refractory lining The method of claim 41, comprising the step of: subjecting the fluid stream to the oxidation chamber to cause thermal oxidation of the components, including the high flow rate of the fluid stream, under some conditions The turbulent flame velocity of one or more fuels in the fluid stream. 47. The method of claim 46, comprising the steps of: reducing the flow rate of the fluid stream below the turbulent flame Speed, whereby the one or more fuels are combusted to reheat the refractory lining. 35 200940155 48. The method of claim 38, comprising the steps of: thermally oxidizing the components and delivering the fluid to the After the downstream device, the fluid stream is removed from the oxidation chamber. 49. The method of claim 48, wherein the downstream device is selected from the group consisting of a processing heater, a boiler, a reaction furnace, an air heater, a group of dryers, gas full wheels, and heat exchangers. 50. A thermal oxidation furnace comprising: an oxidation chamber having a housing and an inner liner defining an open interior a volume and an upstream end and a downstream end; and a heating mechanism for heating the liner and causing thermal oxidation of a component of the fluid stream when a fluid stream is present in the open interior volume, the thermal oxidation being due to the internal The thermal oxidation furnace of claim 50, wherein the heating mechanism includes a burner at an upstream end of the housing for causing one or more of the fluid flow The fuel initially generates combustion to heat the liner and thermally oxidize the one or more components. 52. If you apply for a patent scope! The method of the present invention comprises the steps of: maintaining the conditions during the thermal oxidation of the components such that the degree of enthalpy is maintained below 12 ppm (dry) and the degree of c 维持 is maintained below 1 ppm (dry). 53. The method of claim 3, comprising the steps of: maintaining the conditions during thermal oxidation of the components to maintain the degree of enthalpy below 5 ppm (dry) and maintaining the degree of c 于 at 1 ppm (dry) below. 54. The method of claim 3, comprising the step of maintaining conditions during thermal oxidation of the components such that the degree of helium is maintained at 36 200940155 below 1 ppm (dry) and the CO level is maintained at 1 ppm (dry) below. Η , schema: as the next page 37