LOW NOx BURNER

Abstract: A burner for the combustion of fuel and air in an industrial furnace, for use in connection with preheated combustion air, is provided having an equal number of evenly spaced air jets and fuel jets. The air jets and fuel jets are discharged so that they initially diverge away from one another, but eventually, the fuel jets are entrained by the air jets. During the course of their trajectories, before meeting, the air jets and fuel jets entrain resident furnace gases which results in heavy dilution of the fuel and air before combustion. The dilution causes off-stoichiometric combustion conditions and results in a lower flame temperature. This is similar in effect to external flue gas recirculation. As well, the fuel jets undergo pyrolysis in the course of their trajectories before entrainment occurs. This creates a reducing zone in which the NOx in the resident furnace gases being entrained is reduced, in part, back to molecular nitrogen. NOx emissions from such a burner are shown to be well below that of conventional burners.

Description: Title: Low NOx Burner This a continuation-in-part of United States Patent Application Serial No. 08/451,471 for Low NOx Burner applied for in the name of Frederick K. Besik and Sharhzad Rahbar. Matter disclosed in that application is hereby incorporated by reference into this application. FIELD OF THE INVENTION This invention relates to a burner that provides low level NOx emissions from the combustion of gaseous fuel in air, and in particular is concerned with a burner configuration which curbs NOx formation when the combustion air is preheated to high temperatures. BACKGROUND OF THE INVENTION Natural gas is generally considered one of the most environmentally favourable fossil fuels. The combustion of natural gas can, nonetheless, be the source of undesirable pollutants. The main pollutants from natural gas combustion are oxides of nitrogen, including NO (Nitric Oxide) and NO 2 (Nitrogen Dioxide), collectively referred to as NOx. The impact of NOx on photochemical reactions, urban smog and acid rain is now well-known and documented. Growing environmental concerns have led to increasingly stringent regulations on NOx emission limits throughout the industrial world. Regulatory pressure has prompted substantial research and development aimed at developing combustion systems which substantially reduces the emission of NOx. However, many high temperature industrial operations use the combustion of natural gas as a source of process heat. These industrial operations necessarily result in high fuel gas exit temperatures and high energy losses in the stack. Preheating the combustion air by recovering of heat from the fuel gases can reduce fuel consumption which increases process efficiency and decreases CO 2 emissions. However, increasing the combustion air temperature results in a higher flame temperature. Formation of NOx in the Combustion of Natural Gas The emission of NOx from a combustion system comprising a burner and a furnace depends on the quantities of NO formed and decomposed in the various reaction zones of the flame and furnace. Both the burner as well as the furnace contribute to the formation of NOx. It is generally accepted that formation of NOx in natural gas fired combustion systems occurs by two mechanisms known as thermal NOx and prompt NOx. Thermal NOx refers to the high temperature reactions of nitrogen and oxygen discovered by Zeldovich. The prompt NOx mechanism is thought to occur mainly in the pre-flame zone through reactions involving radicals C 2 , 2 H, CH, CH 2 with nitrogen and oxygen. It is believed that NOx emissions from natural gas combustion are mainly thermal NOx. Thermal NOx formation mechanisms are known to depend strongly on the peak flame temperature and on the concentration and residence time of reactants in the various reaction zones of the flame and furnace. Therefore, the absolute value of the NOx formed from any particular combustion process is determined by the temperature and residence time of the reactants in the high temperature zones. Since the flame temperature increases with increased air preheat, NOx formation has been shown to increase exponentially with the addition of air preheat. The peak flame temperature controlling the formation of NOx depends upon a number of variables including the mixture's stoichiometry, quantity of dilutants present, fuel composition and the initial temperature of the fuel-air mixture. The flame temperature is at a maximum at or near the stoichiometric fuel-air mixture and increases with the combustion air temperature. Maximum equilibrium NOx occurs on the lean side of the stoichiometric point, which is caused by the dependence of the rate of NOx formation upon the temperature, oxygen atom concentration and availability of nitrogen. One method of reducing flame temperature and resulting formation of NOx in conventional burners is to adjust the fuel-air mixture to "off-stoichiometric" - either rich or lean. However, in conventional burners, lean combustion reduces process efficiency and increases fuel costs, while rich combustion results in excess hydrocarbons which must be disposed of by afterburners. As the combustion intensity (energy released per unit volume per unit time) increases, the flame temperature increases, because the volumetric heat loss does not increase proportionally. The larger the capacity of the combustion chamber, the greater the formation of NOx. Combustion intensity is interrelated with equipment capacity. Since flame temperature is increased with increasing oxidant preheat levels, and the process temperature itself frequently already approaches the 1427°C threshold for thermal NOx formation, an exponential increase in emissions of NOx from conventional combustion systems results when oxidant preheat is increased substantially above ambient. Emissions of NOx of around 900-1500 ppm (at 3% excess O 2 ) from conventional burners have been reported at preheat temperatures around 649°C - 816"C. Therefore, for processes which require the combustion of natural gas with preheated combustion air, some means must be provided to reduce NOx emissions to meet regulatory limits. Known Means of Reducing NOx Most of the known methods of reducing NOx emission with high combustion air preheat are commercially unsatisfactory and /or non- viable. Post-combustion treatments are very expensive and carry high cost-penalties per unit of fuel. External flue gas recirculation, requiring extra ducting, insulation, high temperature blowers and controls, is generally considered too expensive to be used with most process heaters. Furthermore, it is impractical to use external flue gas recirculation with processes whose flue products are contaminated. Since even complex burner configurations are less expensive than the additional equipment required for external flue gas recirculation or complicated treatment procedures, it is preferable to prevent as much NOx formation as possible by means of burner design. The configuration of the burner can affect the ratios and mixing patterns of fuel and combustion air in the burner itself, as well as in the combustion and post-flame zones and thus has an important bearing on the combustion process. In particular, the configuration has an impact on the temperature profiles, concentration profiles and residence times through the combustion and post flame zones and thus affects the formation and decomposition rates of NOx. Burner designs that result in intense combustion and higher flame temperatures have been found to produce considerably more NOx than designs that allow combustion to occur in the combustion zones with less intense flames. Attempts to control NOx formation through modification of the burner configuration by way of air staging and fuel staging have shown limited success. Problems encountered with air staging include extended flame lengths and difficulty in achieving low excess air operations. Although fuel staging has been less problematic, neither air staging nor fuel staging have proved capable of meeting the more stringent legislated limits on NOx emissions, without resorting to additional NOx reduction via external flue gas recirculation. Another type of burner which can be used with relatively high combustion air preheat temperature has been developed by the Tokyo Gas Company Ltd, Research and Development Institute. In this burner, gas and air are separately injected into the furnace. The air is injected in six jets equally spaced around and parallel to a central axis. Gas enters the combustion zone in two ways - by an axial jet and by being injected radially into the air jets at the burner face. Optimal NOx - 5 - emissions are said to occur with the fuel flow distribution at 80% axial and 20% radial. The claimed results of 37 ppm NOx emission at 11% O 2 could not be repeated in laboratory tests. The basic teaching in this art is that the air and gas should be directed towards one another, at least to some extent, in order to promote mixing of the air and jets." Even the configuration from the Tokyo Gas Company, mentioned above, has at least part of the two flows directed towards one another. This is understandable, since intuitively, it appears necessary to direct the jets together, to obtain proper mixing, flame stability, etc. SUMMARY OF THE INVENTION Accordingly, it is desirable to provide a burner configuration which can be used in connection with natural gas combustion in air which curbs the production of NOx particularly when the combustion air has been preheated to a high temperature. It is also desirable that such a burner avoid using costly post-combustion scrubbers to satisfy NOx emission limits, and should not require any external recirculation of combustion gases. Additionally, such a burner should preferably be easily adaptable for retrofit. Accordingly, a burner, for combusting a gaseous fuel is provided. The burner comprises: an oxidant supply duct; a fuel supply duct; an oxidant orifice means connected to the oxidant supply duct, for discharging at least one oxidant jet; a fuel orifice means connected to the fuel supply duct, for discharging at least one fuel jet. The oxidant orifice means and the fuel orifice means are arranged such that the oxidant and fuel jets diverge from one another. The divergence is such that the oxidant or fuel jets entrain a substantial quantity of surrounding furnace gases to effect recirculation of the furnace gases and such that the oxidant and fuel jets eventually entrain and mix with one another to form a stable combustion zone. The entrainment of furnace gases effects dilution of the oxidant and the fuel in the combustion zone, thereby lowing temperatures in the combustion zone. In accordance with another aspect of the present invention there is provided: A method of combusting a gaseous oxidant and a gaseous fuel, the method comprising: discharging the oxidant in at least one discrete jet; simultaneously discharging the fuel in at least one discrete jet; adjacent jets of fuel and oxidant being arranged to diverge away from one another such that at least one of the oxidant jet and the fuel jet entrain a substantial quantity of surrounding furnace gases to effect recirculation of the furnace gases, and such that the oxidant and fuel jets eventually entrain and mix with one another to form a stable combustion zone, the entrained furnace gases effecting dilution of the oxidant and the fuel in the combustion zone to lower temperatures in the combustion zone. An important feature of the present invention is the entrainment of one jet by another. For most practical applications, the oxidant will be air, and for this reason, the mass flow of the air will be considerably greater than that of common gaseous fuels. At most practical velocity ranges, the air jets will then have a greater momentum flux than the fuel jets. It is therefore preferred to arrange the fuel jets encircling the air jets, so that the fuel jets are drawn radially inwards and entrained in the air jets. It has proved effective to have equal numbers of air and fuel jets alternating with one another, with the air jets located on one circle, surrounded by the fuel jets on a second, larger circle. However, it will be appreciated that numerous variations are possible. For example, it may prove practical to supply at least part of the fuel through jets aligned with the main air jets and/or at least part of the air through jets aligned with the main fuel jets. Strict alternation of the air and fuel jets may not be necessary for all applications. Further, while the jets should diverge so as to entrain gases, this may not necessarily require the fuel orifices to be located radially, outwardly of the air orifices. For example, the fuel jets, or at least some of the fuel jets could be located within the air jets, with each fuel jet directed between a pair of air jets. Since all the jets have a small section at their base, the fuel jets can pass between the air jets, for sufficient spacing of the jets, with no interaction. Outside the air jets, the fuel jets will then start to become entrained, and curve back towards the air jets. The primary feature of the current invention is the divergence of the fuel and air jets. The divergence is such that the oxidant or fuel jets each entrain substantial quantities of recirculating product gases before the oxidant and fuel jets eventually merge with one another to form a stable combustion zone. These products have had considerable heat taken out of them by radiative heat transfer to the furnace sinks. Thus, before fuel and oxidant begin to react chemically, they are both highly diluted with cooled products, so the attainable combustion temperature is typically very significantly depressed. The dilution of fuel and oxidant with inert product gases in the furnace and the reaction temperature depression accompanying that dilution minimize the residence time of the combusting mixture in high temperature zones, where the formation of thermal NOx occurs, thereby reducing the overall NOx production from the burner. This is similar in effect to that achieved by external flue gas recirculation. Thus the entrainment phenomenon in the pre- combustion zone can be described as "internal flue gas recirculation" as opposed to external fuel gas recirculation. However, this internal flue gas recirculation is much more advantageous as the recirculation occurs inside the furnace enclosure downstream of the burner head without recourse to expensive external ducting to recirculate the fuel gases. When load is applied to the furnace, heat is extracted from the furnace, and the temperature of the resident furnace gases will be reduced. Thus the entrained gases will be at a lower temperature than that of adiabatic conditions. Therefore, it is believed that the addition of load will increase the second effect of the internal flue gas recirculation, causing a further decrease in the flame temperature. Lower flame temperature means less NOx formation, therefore NOx emissions from a burner constructed in accordance with the current invention can be expected to be inversely proportional to load. Such a phenomenon was observed to occur with simulated load via floor heat sinks during experimentation. In addition to the internal flue gas recirculation, in the pre-combustion zone, it is believed that the fuel jets undergo pyrolysis during their trajectories before meeting with the air jets. This creates a reducing zone in which the NOx in the resident furnace gases being entrained is reduced in part back to molecular nitrogen. This is, therefore, a further source of NOx abatement experienced with this burner. The burner of the present invention is advantageous for a number of reasons. The flame is stable, heat distribution is more uniform than conventional burners, and a reasonable turn-down ratio is achievable. The burner is able to withstand high temperatures and is inexpensive to construct. There are no moving parts. A commonly available industrial grade ceramic is used for the ceramic face. The overall burner size is small enough to be suitable for retrofit with existing furnaces. The air and gas pressure requirements are comparable to existing burners In particular the burner does not require a specialized high pressure gas supply, but rather, inexpensive existing supply ducting may be used. Furthermore, the burner is designed for a high temperature furnace with a refractory temperature greater than 900°C and an exhaust temperature greater than 871 °C. As well, there are no problems with start-up. Finally, the burner has been tested in conditions from fuel rich to O 2 content of around 6% in the exhaust gases, and the flame remains stable throughout this zone. BRIEF DESCRIPTION OF THE DRAWINGS For a better understanding of the present invention and to show more clearly how it may be carried into effect, reference will now be made, by way of example, to a preferred embodiment of the present , invention shown in the accompanying drawings in which: Figure 1 is a cross-sectional side view of a burner according to the present invention and as discussed in Example 2; Figure 2 is a front view of the burner of Figure 1; Figure 3a and Figure 3b are schematics of mixing patterns of the air jets and fuel jets emitted by a burner in accordance with the present invention; Figure 4 is a side view of an auxiliary burner in accordance with the present invention; Figure 5 is a schematic of an embodiment of an experimental burner as discussed in Example 1; Figure 6 is a schematic of an embodiment of an experimental burner as discussed in Example 1; Figure 7 is a graph of the effect of combustion air jet angle on NOx for the burners illustrated in Figure 5 and Figure 6; Figure 8 compares the emissions of the performance of the Example 2 burner with commercially available burners; Figure 9 a is a cross-sectional side view of an experimental burner as discussed in connection with Example 3; Figure 9b is a front view of an experimental burner as discussed in connection with Example 3; Figure 10a is a cross-sectional side view of an experimental burner as discussed in connection with Example 4; Figure 10b is a front view of an experimental burner as discussed in connection with Example 4; Figures 11a and lib show a top view and side sectional view of a fuel insert used with the burner of Example 4; Figures 12a and 12b show a top view and side sectional view of an air insert used with the burner of Example 4; - 10 - Figure 13 is a graph of exhaust-gas NOx level versus combustion air temperature with varying exhaust-gas O 2 level for testing result of the Example 4 burner; Figure 14 is a graph of air-temperature-adjusted exhaust- gas NOx level at 3% O 2 dry base versus firing rate for data collected from testing conducted on the burner of Example 4; Figure 15 illustrates the air-temperature-adjusted exhaust-gas NOx level at 3% O 2 versus the firing rate for data collected from testing conducted on the burner of Example 4; Figure 16 graphs the exhaust-gas NOx level against the O 2 level with combustion air temperature as the parameter for data collected from testing conducted on both the burner of Example 3 and the burner of Example 4; Figure 17 illustrates flame radius as a function of distance from the burner exit plane as measured in testing on the flame of the burner of Example 4; Figure 18 illustrates the theoretical model for the angled strong-jet, weak-jet model (SJWJ) used for theoretical modelling of the combustion air dynamics of the burner of the present invention; Figure 19 illustrates fuel trajectories at varying fuel port angles with constant fuel /air momentum flux ratio of 0.02 for the theoretical model illustrated in Figure 18; Figure 20 illustrates the fuel jet trajectories at varying fuel port angles with a constant fuel /air momentum flux ratio of 0.02 on a log-log graph for the theoretical model illustrated in Figure 18. Figure 21 illustrates the relationship between the streamwise point of confluence and the fuel port angle with the fuel /air momentum flux ratio as a parameter for the theoretical model of Figure 18. DESCRIPTION OF THE PREFERRED EMBODIMENTS The following description relates to a non-premix, direct fuel injected burner. The burner is configured to eject oxidant and fuel - 11 - in discrete jets through a number of discrete orifices into the combustion zone. The use of air as the oxidant and natural gas as the fuel is contemplated. It will be appreciated that other oxidant sources can be .used, such as pure oxygen, or oxygen enriched air, as well as other gaseous fuels, but would require the burner configuration to be selected accordingly. Furthermore, the burner is configured to be used with a maximum input firing rate of 400kW. It will become evident that other input firing rates can be used, but would also require the number, size and orientation of the orifices to be selected accordingly. In Figure 1, a burner for use in an industrial furnace is shown generally at 10. Combustion is achieved by the introduction of fuel and air into a mixing zone 40. The oxidant for combustion is provided by the air, and the air may be preheated before entering the burner. The structure of the burner 10 includes an air supply duct 12, a fuel supply duct 14, a central duct 16, a housing 18, a burner block 20 and a mounting flange 22. The burner block 20 is located within the housing 18 in the portion of the burner 10 that is exposed to the furnace chamber. The burner block 20 has an external face 38 which will be exposed to furnace conditions and an internal face 39 which is located within the housing 18. The burner block 20 is formed from an industrial grade ceramic material which insulates the burner's components from the high temperatures in the combustion chamber. The mounting flange 22 is for attachment of the burner to the furnace wall. The housing 18 extends from mounting flange 22 through insulation on the interior of the furnace chamber and into the furnace cavity. The length of the housing 18 is such that a length 17 of the housing 18 protrudes beyond the interior insulation on the furnace walls into the furnace cavity. The air supply duct 12 and the fuel supply duct 14 are circular in cross-section. The air supply duct 12 has a longitudinal axis 42 which is co-axial with the longitudinal axis of the fuel supply duct 14 and the housing 18. The fuel supply duct 14 is smaller in diameter than the air supply duct 12 and is contained within the air supply duct 12. The fuel supply duct 14 extends through the mounting flange 22 and is embedded at one end 15 into the burner block 20. The air supply duct 12 has two sections - an initial source duct 25 and an annular chamber 28. The annular chamber 28 is formed by the housing 18 and the fuel supply duct 14. The air supply duct 12 expands at the mounting flange 22 from the air source duct 25 into the annular chamber 28. The annular chamber 28 ends at the burner block 20. At the internal face 39 of the burner block 20, an internal flange 27 supports the rear of the burner block 20. A ring of holes 26 is provided in the mounting flange 22 to facilitate flow between the air source duct 25 and the annular chamber 28. Combustion air, which may be preheated to an elevated temperature, enters the air supply duct 12 at the mouth of the initial source duct 25 and passes through the ring of holes 26 into the annular chamber 28. Air orifices 30 extend through the internal flange 27, and are embedded in and extend through the burner block 20. There are seven air orifices 30; only one is shown in cross-section in Figure 1. Air exit ports 32 are located at the end of each air orifice 30. Each air exit port 32 has a diameter D 2 . Air is discharged from the annular chamber 28 through the air orifices 30 past the air exit ports 32. Thus air enters the combustion zone in discrete air jets 50. A fuel inlet 24 supplies fuel to the fuel supply duct 14. Fuel orifices 34 extend from the fuel supply duct 14, through the burner block 20 and through the housing 18. There are seven fuel orifices 34; only one is shown in cross-section in Figure 1. Fuel exit ports 36 are located on the housing 18 at the end of the fuel orifices 34. The fuel exit ports have a diameter Di- Fuel is discharged from the fuel supply duct 14 through the fuel orifices 34 past the fuel exit ports 36. Thus fuel enters the mixing zone 40 in discrete fuel jets 52. The length 17 is such that the fuel exit ports 36 clear the insulation on the furnace walls. The burner 10 has a longitudinal axis 42. Each air orifice 30 has a longitudinal axis 44. The longitudinal axes 44 of the air orifices 30 are orientated at some angle, β 2 , from the longitudinal axis 42 of the burner 10. All of the air orifices 30 are orientated at the same angle, β 2 . The air exit ports 32 are evenly spaced around the longitudinal axis 42 of the housing 18 at a constant distance from a point 55, where their axes intersect the longitudinal axis 42 of the burner 10. Similarly, each fuel orifice 34 has a longitudinal axis 46. The longitudinal axes 46 of the fuel orifices 34 are orientated at some angle, βi, from the longitudinal axis 42 of the burner 10. All of the fuel orifices 34 are orientated at β^ The fuel exit ports 36 are evenly spaced axially around the longitudinal axis 42 of the burner 10 and are located at a constant distance from a point 54 where the longitudinal axes 46 intersect the longitudinal axis 42. βi is greater than β 2 . It will be recognized that the longitudinal axes 42, 44 and 46 are also axes of rotational symmetry due to the circular cross-section of the elements involved. Since β r is greater than β 2 , the fuel jets 52 will be discharged externally to the air jets 50. Since both β j and β 2 are inclined away from the longitudinal axis 42, the air jets 50 and the fuel jets 52 discharge divergent from one another. Furthermore, since the diameter D 2 of the air exit ports 32 is greater than the diameter Di of the fuel exit ports 36, the discharged air jets 50 are larger than the discharged fuel jets 52. The air jets must be larger than the fuel jets when using air as the oxidant to achieve combustion because air comprises only approximately 20 % oxygen. If another oxidant is used, appropriately sized orifices would be provided. However, for the desired aerodynamic mixing in the combustion zone, which results in the reduced NOx production, the details of which will be discussed below, it is necessary for the internal jets to be larger and stronger, i.e. to have greater mass and momentum flux, than the external jets. - 14 - Turning now to Figure 2, N a , the number of air orifices 30, is equal to N f , the number of fuel orifices 34. Experiments have shown that equal numbers of air and fuel jets are preferred, as unequal numbers can result in a non-uniform flame. Seven air orifices 30 and seven fuel orifices 34 are shown in Figure 2, therefore N a = N f = 7, although different numbers may bέ used for different thermal inputs. The centre of the fuel exit ports 36 are at a constant radial distance ri from the axis 42. The centre of the air exit ports 32 are at a constant radial distance r 2 from the axis 42. Each fuel orifice 34 is interspaced between two successive air orifices 30 and is equi-distant from each adjacent air orifice 30. For example fuel orifice 34a is located halfway between air orifice 30a and air orifice 30b. The distance between adjacent fuel and air ports is di 2 - The pattern of jets emerging from the burner is fuel-air- fuel etc. with the fuel and air jets diverging from each other and from the longitudinal axis of the burner 10, with the fuel jets to the outside of the air jets. It will be understood from the above discussion of Figure 1 that the configuration of the burner is such that the combustion air and fuel do not mix within the burner itself. Mixing does not occur until the fuel and air are discharged into the mixing zone 40. The pattern of mixing in the mixing zone 40 is determined by the discharge pattern of the air jets 50 and the fuel jets 52 from the burner which, in turn, is influenced by the numbers, sizes and relative arrangement of the air orifices 30 and the fuel orifices 34. Mixing may now be illustrated by reference to Figure 3a. There are three zones within the furnace - a pre-combustion zone 74, a combustion zone 76, and a post-combustion zone 78. When the air jets 50 and the fuel jets 52 enter the pre-combustion zone 74, they do so in a divergent manner with the fuel jets 52 external to the air jets 50 (because βj is greater than β 2 ). However, it is believed that a fuel jet, when discharged between two air jets, will enter the entrainment domain of the air jets, and will eventually split and follow a curved - 15 - trajectory towards the two neighbouring air jets by which they will be fully entrained at a point of confluence 84 in due course. The combustion zone 76 does not occur until sufficient mixing of fuel and air develops at or near the point of confluence 84. Product gases move 5 through the post-combustion zone 78 after combustion is completed. Figure 3b further illustrates the mixing pattern as described above. The air jets 50 are not only larger than the fuel jets 52 but also, the relative supply rate of fuel and air is such that the air jets 50 are stronger and of greater mass and momentum flux than the fuel 0 jets 52, the volume flow of the air jets being approximately ten times that of the fuel jets for natural gas. Therefore the development of the air jets 50 remains largely unaffected by neighbouring fuel jets 52. As each air jet 50 develops downstream of the burner head it is believed its behaviour roughly resembles that of an isolated 5 point-source turbulent round jet which entrains resident furnace gases 80 as it moves through the pre-combustion zone 74. As a result, the fuel jets 52 move through a field of inwardly flowing resident furnace gases 80 which are being entrained by the air jets 50. Because the momentum flux of the fuel jets 50 is relatively small, the trajectories 0 of the fuel jets 52 are affected by the inwardly-flowing furnace gases 80. The momentum of the inwardly flowing gases 80 causes the trajectories of the fuel jets 52 to curve. Eventually, the fuel jets 52 merge with, or become entrained by, the air jets 50. The point at which they merge is called the point of confluence, 84. During the course of 5 their trajectories, the fuel jets 52 also entrain furnace gases 80. Hence, by the time the fuel jets 52 merge with and mix with the air jets 50, both air jets 50 and fuel jets 52 have entrained resident furnace gases 80. It is believed that the aerodynamic mixing pattern of the 0 jets and the resulting entrainment of the resident furnace gases 80 in the pre-combustion zone 74 is the primary factor which results in the reduced NOx emissions from this burner. - I D - Difficulties with the flame stability of this burner, at low furnace operating temperatures, may be encountered. (It is believed that these difficulties are due to the divergence of the air and fuel jets as discussed above.) An auxiliary burner 60, illustrated in Figure 4, is included. As is common in the art, the auxiliary burner 60 is used as a pilot burner for ignition of the main burner 10. However, experimental results indicate that operating the auxiliary burner 60 continuously during combustion, particulary when βi is relatively large, improves flame stability without a creating a penalty in NOx emission. Therefore, for improved flame stability, it is recommended that the auxiliary burner 60 be continuously fired during operation of the burner 10. The auxiliary burner 60 has a main body 62. The main body 62 has an air inlet 64 and a fuel inlet 66 through which air and fuel, respectively, are introduced. Air and fuel are mixed in the interior of the main body 62. Ignition for combustion is provided by a spark electrode 68. The flame produced when the spark electrode 68 ignites the gases is emitted through a pilot orifice 70 at one end, the flame end 69, of the auxiliary burner 60. It will be recognized that the auxiliary burner 60 is structurally similar to known pilot burners commonly used to ignite commercial burners in cold conditions. In fact, the auxiliary burner 60 of the present invention also functions as a pilot burner. It will be evident that other suitable pilot burner structures may be substituted for that as illustrated in Figure 4. Referring back to Figure 1, the auxiliary burner 60 is placed inside the central duct 16. The central duct 16, co-axial with the housing 18, extends from behind the mounting flange 22 and is embedded in and extends through the burner block 20. The flame end 69 of the auxiliary burner is not flush with the external face 38 of the burner block 20 but rather is located within the burner block 20 at some distance 71 from the external face of the burner block 38 so that a portion of the burner block 20 acts as a flame holder for the auxiliary burner 60. The distance 71 must be at least one inch to prevent lift off of the flame. The materials used to construct this burner must withstand high temperatures encountered during its operation. In the preferred embodiment, all elements, except for the burner block 20, are constructed from high temperature stainless steel. In particular, the air orifices 30 and the fuel orifices 34 are lined with stainless steel with a grade of SS316. The burner block 20 is made from an industrial grade refractory ceramic material able to withstand high temperature conditions. It will be understood however, that the other suitable temperature resistant materials can be substituted. Although in Figure 1 the air exit ports 32 are located on the external face 38, and the fuel exit ports 36 are located on the housing 18, it will be understood that in other embodiments, the location of either of these two types of exit ports, on either the burner face or the housing, will depend on the precise location of the relevant orifice, the angle at which the orifice is orientated, and the dimensions of the burner block itself. Furthermore, other ducting arrangements of the air supply duct, the fuel supply duct, etc may be used to feed the orifices as disclosed. Further, the burner block need not be perfectly cylindrical. Its end face could be a three-dimensional curved surface, which could be shaped so that all the orifices are perpendicular to the surface. Further, it may not be necessary for the orifices or jets to diverge from one another. If the jets are placed sufficiently far apart, it may not be necessary to direct them away from each other (and it may in fact be necessary to direct them towards each other). In this case, subject to appropriate mixing to achieve a stable flame, the jets will still entrain resident furnace gases before mixing, diluting the jets, thereby lowering the flame temperature and decreasing NOx emissions. It may also be possible for the orifices to be provided in a variety of different shapes and patterns, e.g. slot, annular etc. - Iσ - The preferred embodiment as described has the number of air orifices equal to the number of fuel orifices, N a = N f = 7. It will be recognized that for maximum nominal inputs other than 400kW, N a and.N f will be selected as is appropriate. Furthermore, for some cases, it may not be necessary to have any precise correspondence between the number of oxidant jets and fuel jets. While the preferred embodiment is directed to NOx formation from the combustion of natural gas in air, it is to be recognized that the burner configuration can be used with respect to any fuel that emits NOx or other pollutant whose formation depends upon the flame temperature. EXPERIMENTATION KEY TO VARIABLES di 2 - distance between centres of exit of adjacent fuel and air ports of a burner, mm Di - burner fuel port diameter, mm D 2 - burner air port diameter, mm m a - mass flux of combustion air, kg/s m e - mass flux of exhaust gas from the combustion chamber, kg/s πi f - mass flux of fuel (natural gas), kg/s m f (-Δh c ) - standard rate of combustion heat release, W N a - number of air ports N f - number of fuel ports ri - radial position (from the burner axis) of the centre of a fuel port at exit, mm r 2 - radial position (from the burner axis) of the centre of an air port at exit, mm S b - total surface area of bare floor sink panels, m2 S c - total surface area of covered floor sink panels (covering was of 25.4 mm thick refractory insulation, sold under the trade mark Cerablanket), m 2 S n - surface are of cold sink at nearfield port, for flame detection trials T a - temperature of combustion air at burner entry, °C T r - refractory surface temperature, °C β j - angle between fuel port axis and burner axis, deg β 2 - angle between air port axis and burner axis, deg α - off-set angle of fuel ports - 1 ι Q y - PCT/CA96/00334 Theoretical Modelling Variables D 0 - jet port diameter (either Di or D 2 ), m N - number of Jets, = 1, .\ one fuel jet, one air jet m e - • mass flux of ambient fluid entrained by either jet, kg/s m D - the port (feedstream) mass flux in either jet, kg/s Ui - = Gι/mι, mean port velocity of feedstream 1, m/s; U 2 = G 2 /m 2 , mean port velocity of feedstream 2, m/s; x, y, z cartesian coordinates for the problem X c distance from the starting plane ("burner face") to the meeting point of the trajectory of the weak ("fuel") jet with the edge of the strong ("air") jet, m [The effective streamwise position of the point of confluence of the jets.] y 0 distance between the centres of the jet ports at exit, characteristic length scale for the problem, m yι /C lateral position of the meeting point of the trajectory of the weak ("fuel") jet with the edge of the strong ("air") jet, m β a angle between the starting plane and the port axis of the weak jet (the "fuel" port angle), deg β b angle between the starting plane and the port axis of the strong jet (the "air" port angle), deg, β b = 0° for this model η = y/y 0 , dimensionless cross-stream coordinate, 1 ξ = x/y 0 , dimensionless streamwise coordinate, 1 ξ c X c /y o / dimensionless distance to the point of confluence of the jets, 1 p e density of the gas (the ambient fluid) entrained, kg/m 3 ψ = Gι/ G 2 = mιUι/m 2 U 2 , momentum-flux ratio of the weak ("fuel") and strong ("air") jets, 1 PRELIMINARY EXPERIMENTATION A number of different burner geometries were constructed and tested to determine the effect of fuel /air discharge pattern. Axial jets, both air and fuel were compared to radial jets of the same. Annular fuel flow was explored. (Annular fuel flow was achieved by introducing fuel into the burner block fuel chamber tangentially via a single fuel port into an annular duct to achieve rotation of the gas and a symmetric annular fuel discharge into the combustion zone. The tangential introduction gave a swirl component to the fuel flow in the duct, so that at the discharge it diverges into a conical flow shape.) As well, a burner in accordance with the concept developed by the Tokyo Gas Co Ltd. R & D Institute was constructed having six external axial air jets combined with a central fuel jet and six radial fuel jets injected tangentially into the air jet streams. (Attempts to repeat the NOx results claimed by the Tokyo Gas Company as described in "Fuel Direct Injection Low NOx Combustion Technique" by Tokyo Gas Co Ltd, 1989 International Gas Research Conference. Tokyo Japan, 6-9 November, 1989, were unsuccessful.) As far as the effect of the fuel flow pattern goes, the preliminary testing showed that axial fuel jets produced considerably higher NOx levels than the radial fuel jets. This is contrary to the results presented by the Tokyo Gas Company which indicate that NOx production is optimal at a fuel distribution of 80% axial and 20% radial. The radial fuel jets and the annular fuel discharge produced similar NOx levels. Conventional industry know-how predicts significant stability problems if more than 20% of the fuel is introduced externally to the oxidant. EXAMPLES Examples of burners according to this invention are described in detail in Examples 1-4. Studies were performed to evaluate performance of the burners with preheated combustion air as well as with other operating conditions. Results of these tests are included and discussed where appropriate. Unless otherwise specified, all trials were run with 15% excess air, which is equivalent to 3% excess O 2 on a dry basis (d.b.) in the exhaust gas. Natural gas was used as the fuel in all cases. EXAMPLE 1 - DEVELOPMENTAL BURNERS The Example 1 burners were constructed for a maximum input of 65kW. Figure 5 illustrates the structure of an Example 1 burner. The structure of this burner is similar to that illustrated in Figure 1 and the reference numerals of Figure 1 have been repeated where appropriate. The Example 1 burners have six air orifices 30 orientated at 0°, (β 2 =0°) from the longitudinal axis of the burner 42 and six fuel orifices 34 orientated at 65° (βj =65°) from the longitudinal axis of the burner 42. The fuel orifices 34 are interspersed between adjacent air orifices 30. The diameter of the housing 18 is 152mm. There are some structural differences in example 1 as compared to the embodiment shown in Figure 1. The burner block 20 of Example 1 extends back to the mounting flange 22 and beyond into the air source duct 25. This obviates the need for the internal mounting flange 27 and results in there being no annular chamber 28. Instead, the air and fuel orifices 30 and 34 extend throughout the burner block 20, with angled portions 101 at the end of the fuel orifices 34 to discharge the fuel jets 52 at the desired angle. Fuel is supplied to the fuel orifices 34 by a fuel supply ring 102. Figure 6 illustrates a second Example 1 burner. This burner is identical in structure to the that shown in Figure 5, except that the air orifices 30 are orientated at 10°, (β 2 = 10°). The tests were carried out in a test facility that was essentially conventional. It included an independent high temperature combustion air preheater, a combustion tunnel, fuel gas collection-dilution-discharge system and appropriate sampling and analysis equipment. The actual tunnel was of square cross-section with an area of 0.51m by 0.51m and an inside length of 2.1m. The tunnel was lined with refractory material in known manner. The front end of the tunnel had a circular opening for mounting experimental burners. Figure 7 is a graphical summary of data collected, showing NOx emissions for the inputs of 65 kW at combustion air temperatures of 632°C, plotted against the surface temperature of the tunnel wall. Curve A corresponds to data from testing with the Example 1 burner of Figure 5. Curve B corresponds to data from testing with the Example 1 burner of Figure 6. Curve A and Curve B indicate that air jets at an angle of about 10° from the burner axis, are more effective in reducing NOx than the axially discharging air jets (β 2 = 0°). EXAMPLE 2 - 400kW BURNER Example 2 was a scaled up prototype designed for maximum input levels of 400 kW. "" The purpose of Example 2 was to develop an optimized burner configuration which resulted in maximum NOx emissions of 30 ppm at 3% excess O 2 , while operating with 650°C air pre-heat and furnace temperatures of 1538 °C to 1700 °C. The configuration of Example 2 is the same as is illustrated in Figure 1 with the following dimensions and characteristics: Orifice Configuration βi = 65° β 2 = o° Di = 6.22 mm D 2 = 18.42 mm ri = 110 mm r 2 = 87.3 mm N a = N f = 7 Testing was completed for the above burner in a larger testing facility similar to that mentioned before, with a square cross- section area of 1.14m 2 and inside length of 4.9m. No heat sink was provided except that provided by the refractory walls which were lined with 20cm thick refractory blanket insulation. Performance data illustrating NOx results in testing of this burner is contained in Table 1. All tests were run at excess 0 2 levels in the exhaust gas of 3%. TABLE 1 Performance of the Example 2 Burner Nominal Input : Air Preheat %co 2 NOx ppm CO ppm Test kW • c dry (3% 0 2 ) (3% 0 2 ) No. 450 649 10.4 13 δ 29 450 316 10.5 9 11 30 450 149 10.6 7 11 31 450 ambient 10.5 7 9 28 300 649 10.6 9 7 21 300 316 10.4 8 6 20 300 149 10.6 6 8 23 300 ambient 10.5 6 8 22 150 649 10.5 7 7 24 150 316 10.6 7 8 26 150 149 10.1 6 7 27 150 ambient 9.7 6 10 25 Figure 8 shows a comparison of these results with the NOx emissions experienced with commercially available burners. NOx emissions from the Example 2 burner are significantly below those of commercially available burners. Furthermore, in conventional burners NOx emissions increase exponentially with an increase in combustion air preheat temperature. With the Example 2 burner, however, although there is an increase in NOx with rising air preheat temperature, it is a very gradual increase which appears to be linear. EXAMPLE 3 The Example 3 burner was constructed to conduct further investigation into burner performance and, in particular, to investigate the effect of fumace geometry on the flame. The Example 3 burner is illustrated in Figures 9a and 9b. The Example 3 burner is similar in structure to the embodiment illustrated in Figure 1 and reference numerals have been repeated where appropriate. The dimensions and characteristics of the Example 3 burner are as follows: Orifice Configuration Basic Burner Configuration β, = 65° Diameter of air source duct 25 = 152.4mm β 2 = 10° Diameter of fuel supply duct 14 = 89mm Di = 22 mm Diameter of central duct 16 = 35mm D 2 = 15.88 mm Diameter of housing 18 = 110mm ri = 110 mm Length of housing 18 = 362mm r 2 = 87.3 mm Longitudinal location of fuel ports 36 = 12.7mm N a = N f = 7 Length of burner block 20 = 79.4mm Mounting Flange 22, = 483mm x 483mm square Length of auxiliary burner 60 = lm It is evident from Figures 9a and 9b that there are some structural differences between the Example 3 burner and the embodiment discussed in Figure 1. The Example 3 burner includes an external refractory portion 103 which was included to fit the burner with the furnace port and does not form part of the present invention. The furnace used for testing of the Example 3 burner was much larger than the ones used previously. It allowed for firing of three burners side by side and for the simulation of load by extracting heat from the furnace through a water cooled floor. The internal cavity of the furnace was lm by 3m by 4.5m. In order to obtain data comparable to the previous Example burners, internal refractory brick walls were placed inside the furnace chamber during some of the trials to vary the furnace chamber size. Sink was provided by bare floor sink panels. To vary sink, portions Of the bare floor sink panels were covered with 25.4mm thick refractory insulation, sold under the trade mark Cerablanket. Some trials were operated with the sink panels fully covered to attempt to reach adiabatic or zero sink conditions. However, the insulation did not fully reduce heat flow to the sink panels, therefore, an assumption of zero sink conditions is an approximation. Table 2 summarizes the operating conditions and NOx results for the testing of this burner. S b denotes the total area of bare floor sink panels used throughout the tests and S c denotes the total area covered by the refractory insulation. TABLE 2 Results and Operating Conditions of the Trials with the Example 3 burner Trial Combustion Chamber H x W x L, s , s„ πif, max T a *, Oz, NO x , m x m x-m m2 m2 g/s • c % d.b. p m , d.b. 1 1 x 1.5 x 3 0 4.5 4.9-6.9 418 1.6-6.7 16-22 2 1 x 1 x 3 0 3 6.9-7.8 392 1.5-2.9 10-47 3 3 1 x 1 x 3 0 3 6.1-7.8 402 1.1-3.5 14-46 4 1 x 1 x 3 3 0 6.0-7.8 263 8.2-9.0 — 5 1 x 1 x 3 3 0 7.7-8.0 267 3.9-7.9 4-10 6 1 x 1 x 3 0.75 2.25 5.9-7.9 338 1.6-10.2 11-18 7 1 x 3 x 4.5 0 13.5 6.0-7.8 356 0.0-4.8 8.5-16 8 1 x 1.5 x 3 0 3 5.8-7.8 392 1.1-3.2 14-25 9 1 x 3 x 4.5 13.5 0 7.9 181 6.6-6.8 5 10 1 x 3 x 4.5 1.5 12 6.1-7.9 345 3.5-10.6 3-7.5 The quantity max T a is the highest level reached by the air temperature during the trial. ,,,---, PCT7CA96/00334 - 26 - In these trials, the excess air level was maintained at 3% o 2 . The results of Table 2 indicate that burner performance was affected by furnace volume. When the burner was fired in a furnace volume comparable to the volume used in Example 2, lower NOx values, similar to those produced by the Example 2 tests were realized. However, when fired in a furnace volume smaller than Example 2 (trials 2, 3) the NOx levels exceeded the Example 2 values and reached 47 ppm at 3% 0 2 . It is believed that one factor in this phenomenon is the use of a fuel angle of β, = 65°. The larger the fuel angle β t , the farther the fuel jets 52 travel away from the air jets 50 before the trajectories of the fuel jets 52 curve and move back towards the air jets 50. This in turn results in a larger flame volume. It is believed that, with larger fuel angles βi, in smaller furnace chambers, the fuel jets will impinge on portions of the furnace interior before they are entrained by the air jets. Thus the fuel jets do not cleanly arc over to be entrained by the air jets and instead, a complex process of mixing and reaction ensues and the flame extends through a greater volume of the internal furnace chamber. Therefore, one of the limitations on the fuel angle βi , will be the configuration of the furnace chamber within which the burner is to be used. For optimal performance, particularly of the flame, the fuel port angle γ should be chosen so that the fuel jets are substantially entrained before they reach the internal surface of the furnace chamber. Therefore, it is concluded from the results of the Example 3 burner that although a fuel angle of 65° shows favourable NOx values, such an angle does have a significant effect on flame stability. Lower fuel angles serve to tighten the flame, lowering its volume. EXAMPLE 4 It was desired to test the effect of varying burner parameters without constructing a new burner each time. Therefore, a further experimental burner was constructed with air and jet orifices designed to accommodate threaded inserts so that the angle and diameters of the air and fuel ports could be varied. The construction of a burner with variable inserts was to facilitate experimentation with varying burner configurations, and is not recommended for commercial use. The burner body of the Example 4 burner is shown in Figures 10a and 10b. Its construction is very similar to that of the Example 3 burner and the preferred embodiment and therefore equivalent reference numerals have been repeated where appropriate. One significant difference in the structure of the Example 4 burner is found in the fuel and air orifices 34 and 30. The apertures in the burner block 20 which surround the orifices were widened and provided with internally threaded bores shown as 110 and 112 for the air and fuel respectively. The internally threaded bores 112 for the fuel orifices are orientated at an angle of 50° from the longitudinal axis of the burner 42. The internally threaded bores 110 for the air orifices are orientated at an angle of 10° from the longitudinal axis of the burner 42. To vary the diameter of the orifices and the angle of ejection of the jets, externally threaded inserts were constructed. A fuel insert 114 with an aperture 115 is illustrated in Figure 11. The aperture 115 provides the effective fuel port diameter Di. The aperture 115 is inclined from the longitudinal axis 116 of the insert 114 at an angle α. The insert 114 is designed to be received by a threaded bore 112 of Figure 10a so that the combination (of the angle of 50° of the threaded bore 112) and angle α results in the desired fuel jet angle β,. An air insert 118 is illustrated in Figure 12. The insert 118 has an internal aperture 120 and is designed to be received by a threaded bore 110 of Figure 10a. Variation in the diameter of the insert 120 enables variation of the effective air port diameter Di. Since the air jet angle, β 2 was not varied, it was not necessary to incline the - 28- aperture in the air insert 118 as the threaded bore 110 was already inclined at 10°. The specifications of the Example 4 burner, including the variations in βi, and D 2 that were utilized, are summarized as follows: Jet Configuration Burner Configuration β ! = 30°, 35°, 42.5°. 65 c Diameter of air source duct 25 = 152.4mm β 2 = ιo° Diameter of fuel supply duct 14 = 89mm Di = 6.35mm Diameter of central duct 16 = 35mm D 2 = 15.88mm Diameter of housing 18 =216mm 19.05mm Length of housing 18 = 394mm 24.31mm Length of burner block = 76.2mm ri = 86 mm Mounting Flange 22 = 483mm sq. by 6.35mm r 2 = 86 mm Length of pilot burner 60 = lm N a = N f = 7 Again, an external refractory portion 103, similar to that discussed in connection with the Example 3 burner was included. The Example 4 burner was tested in the same furnace as the burner of Example 3. However, only one furnace chamber configuration, lm high by 1.5m long by 3m long, was employed in these trials. To obtain a full measure of its effects, the excess air level was varied from 2% to 30%, corresponding to exhaust gas 0 2 from zero to over 5% on a dry basis (d.b.). The entire floor was covered with Cerablanket insulation to approximate operation without sink and this was not varied. As well, there was no variation in recuperating operating conditions. Thus, operationally, the controlling variables were firing rate, excess air level and combustion air temperature. Accordingly, a correlation between those three variables and NOx emission was investigated. Operating conditions of the burner are summarized as follows: TABLE 3 Results and Operating Conditions of the Trials with the Example 4 Burner Trial Di D 2 β. m_, Ta*, TΛ o ∑ . NO,, mm m m deg g/s max, * C max, "C % d.b. p pm d.b. 1 6.35 15.87 35 3.0-7.1 400 1281 0-4.9 3.4-29 2 6.35 15.87 35 6.2 399 1278 0.8-1.9 17-26 3 6.35 19.05 35 4.3-7.9 320 1231 0-2.4 2.8-26 4 6.35 25.40 35 3.1-8.0 379 1326 0-1.8 18-42 5 6.35 19.05 30 1.5-7.6 389 1290 0-5.1 5.8-30 6 6.35 19.05 42.5 1.9-8.0 341 1252 0-3.5 8.5-24 7 6.35 19.05 30 1.8-8.9 377 1290 0-3.9 3 . 3 - 3.4 *The quantity max T a is the highest level reached by the air temperature during the trial. The quantity max T r is the highest surface temperature reached at the hottest spot of the refractory. During the trials, observations were made on flame performance. Table 4 summarizes these observations on combustion stability and flame appearance. TABLE 4 Flame performance in the adjustable burner tests: Observations on combustion stability and flame appearance in trials with the Example 4 burner. Burner parameters not varied: Dj = 6.35 mm, β = 10°. Pi, D 2 , Auxiliary Turndown limit 3 , Remarks deg UUl burner % of full fire 42.5 19.05 On 26, control limit Good flame, no luminosity Off 40, flameout Good flame, some luminosity 35 24.31 On 42, lowest set Good flame, slight to small luminosity, NO x elevated by 50—65% over case at D 2 = 19.05 mm Off 71, flameout Good flame, NO x elevated as with pilot on 35 19.05 On 42, lowest set Good flame, occasional slight to small luminosity Off 71, flameout Good flame, no luminosity 35 15.85 On 42, lowest set Good flame, slight luminosity at higher 0 2 levels Off Not tested 30 19.05 On 24, control limit Good flame, no luminosity Off 20, control limit Good flame, no luminosity. Turndown behaviour is that observed in Trial 950215, when more results were obtained for the same operating c onditions, flameout was experienced at 71% of full fire; however, the burner was at this point exhibiting symptoms of deterioration from scaling (burning out), so this experience, at variance with 950210, is suspect. a Nominal full (100%) firing rate set at 350kW, the maximum attained in single-burner operation of the Example 4 burner. - 32 - The results indicate that diminishing the fuel angle βj and maintaining the air port diameter D reasonably small (thereby resulting in high air jet momentum flux) improves flame stability without a significant adverse effect on NOx emissions. According to the theoretical model of the entrainment aerodynamics of this burner, discussed below, both measures tend to advance the entrainment of the fuel jets by the air jets and shorten the flame. Table 4 also raises the question of continuous operation of the auxiliary burner. With the pilot off, the best results are with βi = 30°, the smallest fuel port angle tested. It is predicted that smaller values of βi will improve combustion stability subject to a minimum limit on βi beyond which NOx emissions begin to rise and reach unacceptable levels. RESULTS Figure 13 is a graph of the exhaust-gas NOx level as a function of the combustion air temperature as the exhaust gas 0 2 level is varied with the firing rate in the range from 289kW to 368kW. Burner parameters were β j = 30°, β 2 = 10°, Di = 6.35mm and D 2 = 19.05mm. The pilot burner was on. Based on Figure 13, the relationship between NOx level as a function of air temperature, with the 0 2 level as the parameter can be expressed by the following equation: [NOx] = CT a 1 * 44 / where C is a function of the 0 2 level (Eq.l) for 200°C < T a < 600°C, except when: T a < 300°C at [O 2 ]=0%, T a < 275°C at [O 2 ]=0.5%, and T a < 250°C at [0 2 ]=1% It was observed that at low O 2 levels NOx production drops off sharply as combustion reaches fuel rich conditions which is consistent with known behaviour of conventional burners, but which is also known to be impractical for reasons of pollution. Assuming equation 1 is valid for firing rates throughout the turndown range, correction can be made for the temperature effect. Figure 14 is obtained by correcting data for other air preheat temperatures to NOx emissions for 400°C to determine the effect of turndown in the firing rate alone with constant exhaust gas O 2 level of 3%. Figure 14 illustrates that turndown in the firing rate over a 4:1 range significantly decreases NOx emission. A power law is postulated for the relationship illustrated in Figure 14 as follows: [NOx] 4 oo ° c, 3%0 2 = C[m f (-Δhc)]n (Eq.2) where: n=0.58 for βj = 30°, n=0.38 for β,. = 42.5° D 2 constant at 19.05mm Figure 15 was obtained by correcting NOx emissions for T a = 400°C for trials in which β,. = 35° and βj = 30°. Equation 2 seems to hold for these plots except for a deviation at the lowest firing rate. The exponent n=0.81 for D 2 = 15.88mm and 19.05mm, but n decreases to 0.58 at D 2 = 24.3mm. The curve A in Figure 15 represents data which has been temperature-correlated to 400°C, for βj = 35° and D 2 = 15.88mm and 19.05mm. Curve C represents the same data for βj constant at 35° but D 2 = 24.3mm. Comparison of curve A to curve C in Figure 15 shows that NOx levels are significantly elevated when the air port diameter D 2 is increased. It is believed that the diameter of 24.3mm lowered the air jet momentum flux to the point where the postulated entrainment of the fuel gases was no longer occurring or was significantly reduced, thus adversely affecting NOx. (Theoretical modelling, discussed later, predicts that the air jet momentum flux is an important factor in the entrainment phenomena which results in the low NOx emissions from burners with the configuration of the present invention.) The dotted curve, curve B, in Figure 15 represents the temperature-correlated data for β ! = 30° and D 2 = 19.05mm. Comparison of curve A to curve B in Figure 15, reveals that NOx emission at β ! = 30° is significantly elevated and that decreasing β j from 35° to 30° adversely affects NOx. The adverse affect on NOx must be weighed against the benefits of lowering βj to increase combustion stability and to obtain smaller flame size. The data for a firing rate of about 300kW with λ = 30° , Oι = 6.35mm, β 2 = 10° and D 2 = 19.05mm can be represented by the equation: [NOx] 40 o ° = 20 + 8.5[O 2 ]0.577, ppm (Eq.3) where the 0 2 level is in % and ranges from 1.5-2.4% d.b., and both NOx and 0 2 are on dry basis. Equations 1, 2 and 3 can be combined to postulate a general representation of NOx levels as a function of 0 2 level, firing rate and air temperature as follows: [NOx] = (20 + 8.5[O 2 ] 0 -577)(T a /400)i-44( mf (-Δh c )/300)0.58 (Eq.4) for β t = 30° Di = 6.35mm and D 2 = 19.05mm β 2 = ιo°. This correlation is roughly accurate for all trials, excluding the trial with the large air port diameter of D 2 = 24.3mm. It is estimated that the range of practical reliability is somewhere in the ranges of: 0 < [0 2 ] < 7% d.b., 200°C <T a < 600°C, and 50 kW < m f (-Δh c ) < 500 kW. However, this correlation is intended to give only a guide to and an appreciation of the effects of the operating variables. It is limited to the structure, system and operating conditions used in compiling the data on which it is based, and does not approach a fundamental explanation of the burner. Figure 16 illustrates the exhaust gas NOx level as related to the 0 2 level with variable combustion air temperature. The smooth curves are from data obtained from testing with the Example 4 burner. The data indicated by discrete points in Figure 16 was obtained from testing of the Example 3 burner. Agreement between the Example 3 results and the Example 4 results is close at the lower air temperatures, but the NOx levels reached with β^ 65° at the highest temperature are somewhat elevated indicating that, at high temperatures at least, β^ 65° is less desirable. Preliminary studies were undertaken to investigate the location of the flame from the Example 4 burner. The burner specifications were Di = 6.35mm, D 2 = 19.05mm, β- = 35° and β 2 = 10°. The burner was operated at full fire into the full furnace. Operating conditions for the three individual cases were as follows: TABLE 5 Operating conditions of the nearfield trials with the Example 4 burner. Control settings (firing rate, excess air) were not varied within a set of trials, so only small variations in operating conditions occurred (those associated with incomplete approach to steady state, with changes in atmospheric pressure and temperature, and with the limitations of the control system itself)- Burner parameters: Dj = 6.35 mm (1/4"), D 2 = 19.05 mm (3/4"), βi = 35 * , β 2 = 10°. Auxiliary burner: on. Combustion chamber: the full furnace. Case: A B Ω Remarks Sb 2 m2 0 1 0 — S c m2 13.5 12 13.5 -- S n m2 3 0 0 Nearfield door & port Exhaust O^ % d.b. 3.7 2.6 2.7 — mfkg/s 0.00655 0.00653 0.00646 — ma, kg/s 0.1287 0.1212 0.1205 — m f (-Δh c ), kW 313 312 309 — Qs,b, kW 0 75.5 0 — Qs,c- kW 50.1 59.0 88.2 — T a , °C 299 332 380 -- max T r , °C 880 1019 1139 -- The flame boundary was assumed to be determined by where the time-mean CH 4 content effectively drops to zero, as in a turbulent natural gas-diffusion flame, the bulk of combustion heat release .and most of the CO oxidation occurs within the zone where CH 4 is detectable Figure 17 shows 'the lateral (horizontal or vertical) maximum R f (in mm) of the CH 4 content as a function of the distance x x (in mm) from the burner exit plane. The Case A flame actually impinges upon the sidewall of the furnace, so the length it might otherwise have in a furnace of adequate size to avoid this condition is not directly evident. The Case A illustrated in Figure 17 is an estimate of what the Case A profile would be in a furnace large enough to avoid the impingement problem. MULTIPLE-BURNER TRIALS Tests were also conducted with three of the Example 3 burners fired side-by-side. The results showed that three burners of the present invention can be fired side-by-side with no adverse effect on flame stability. Therefore, confirming that the present burner is suitable for multi-burner firing. The NOx emissions under air preheat conditions remained well below the most stringent regulated limits, never exceeding 10 ppm @ 3% 02 in the flue. However, the NOx emissions were found to be double that of a single burner. It is believed that the presence of adjacent burners interferes with the entrainment process resulting in less entrainment of furnace gases and consequently NOx formation not being reduced to the same extent as in the single burner trials. It is believed that if the burners are spaced from one another appropriately, it will be possible to minimize this effect, subject of course to physical limitations within the furnace. However, in a long furnace with a row of burners and product gas flow transverse to the burners, a substantial gradient may occur in the temperature for the recirculating products being entrained by the flame jets. In this case, NO x emission may increase (due to the higher temperature of the products being entrained) even if appropriate spacing is used. This holds true for other burners as well and is a reflection of the interaction between burner and furnace. SINGLE TET MODELLING The present invention contemplates multiple jets in both air and fuel. However, a simplified two-jet mixing pattern has been examined to provide a model and rough guide to the more complex behaviour of the multiple jet scenario. The model examines the mixing behaviour of an angled strong-jet, weak-jet (SJWJ) interaction. As illustrated in Figure 18, the model is chosen with number of fuel and air jets N=l. A strong air jet 120 issuing normal to the exit plane (β b = 0). At a distance yo away, a weak fuel jet 122 issues from the exit plane at an angle β a to the normal. (Strong and weak are in the sense of momentum flux.) Typically, the burner exit velocities, U i and U 2 are similar, but the fuel jet is weaker since typically combustion of natural gas occurs on the air-rich side of stoichiometric. Thus, the fuel/air momentum ratio ψ is typically small. Entrainment is taken to occur effectively at the distance x = x c where the fuel jet trajectory meets the edge of the air jet. It is assumed that the strong air jet is negligibly disturbed by the weak fuel jet and thus develops like an isolated free jet in a stagnant ambient gas, as if the fuel jet was not present. The air jet entrains ambient gas and so grows in mass flux as it moves in the x direction. The fuel jet on the other hand moves through a field of ambient gases flowing radially towards the air jet as a result of being entrained by the air jet. The fuel jet also entrains ambient gases, but those ambient gases have a component of velocity towards the air jet. Thus the fuel jet develops an increasing component of momentum towards the air jet and describes a curving trajectory closing in upon the air jet. At some point x c , known as the point of confluence, the fuel jet meets the air jet and is entrained by it. Figures 19 and 20 illustrate the behaviour of the fuel jet trajectory over a range of angles β a = 0-40° at a fuel/air momentum flux ψ = 0.02 (a typical momentum flux ratio expected with these types of burners). The normalised streamwise and cross-stream co-ordinates are η = y/yo and ξ = x/yo . Figure 20 is a log-log graph which shows the „_-,-„ PCT/CA96/00334 - 39- point of confluence for all cases. (The shape is of course distorted). The effect of fuel port angle β a on the point of confluence x c is very strong, increasing by an order of magnitude as β a approaches 40°. Figure 21 illustrates the relationship between the streamwise point of confluence ξ c = x c /yo and the fuel port angle β a with the fuel/air momentum flux ratio ψ as a parameter. Over the ranges β a = 15-40° and ψ = 0.005-0.08, the curves of Figures 19 and 20 are well-fitted by the equation: X c = 6.5y 0 ψ o-i exp(0.01 25 β a 2 ψ l /2) (Eq.5) The analysis shows that, for β a = 0-40°and for momentum flux ratios ψ of the order of 0.02, the mass flux of the ambient fluid entrained by either jet up to the point of confluence, is, to a close approximation, m e = 0.32m o (x c /D o )(p e /p o ) 1 /2 (Eq.6) where m 0 = source flux (feeding either the fuel jet or air jet) D 0 = source port diameter (round orifices) p e = density of fluid being entrained (furnace gases) p 0 = density of source fluid (air or fuel) Since usually x c /D 0 » 1, substantial dilution by entrainment can be expected. Furthermore, since the fuel port will generally be smaller than the air port, x c /D 0 will be larger for the fuel jet and thus more entrainment will occur. It should be emphasized that this gives only a rough prediction of behaviour of the present invention and depends on a number of theoretical assumptions and simplifications. Influences of adjacent jets on one another in a multi-jet environment can be expected to have an affect on the behaviour of the jet mixing patterns. Other factors, the angle of the air jet in particular, can also be expected to influence the interaction of the jets. The model and equations can be applied to one of the data trials of Example 4. In this trial, the conditions were as follows: _, -, PCT/CA96/00334 • 40 - Momentum flux ψ = 0.0179 Density of fuel p = 0.737 kg/m3 Density of air p a = 0. 498 kg/πv* Density of exhaust gas p e = 0.201 kg/m3 (estimated) β, = 35° β 2 = 10° n = r 2 = 86mm Di = 6.35mm D 2 = 19.05mm To apply the modelling equations, β a is trigonometrically determined from β ! and β 2 to be 26.3°. Similarly, yo, equivalent to dχ 2 , the absolute distance between a pair of adjacent air and fuel jets, is trigonometrically determined as 38.3mm. Substituting in, ignoring the effects of multiple jet interactions, the model equations predict: x c = 529mm (from Eq.5) m e /m f = 13.9 for the fuel jets (from Eq.6) m e /m a =5.65 for the air jets (from Eq.6) Thus, the entrainment ratios indicate that before the fuel and air jets meet, and the flame properly begins, the fuel is on average, diluted with combustion products at a rate of 13.9 kg/kg and the air is diluted with 5.65 kg/kg. This is a strong effect which achieves "fuel gas recirculation" via combustion aerodynamics within the internal chamber of the furnace. No external ducting is required. It should be noted that when excess air is used, the products gases will contain some oxygen. Thus the fuel jets which entrain this oxygen will begin some preliminary combustion before the point of confluence. In the example above, suppose the excess air level is 15%. In that case, the 13.9 kg of product gases entrained per kg of the fuel jet, contains 0.400 kg of oxygen compared to the 3.81 kg required for complete combustion. Thus this is a fuel-rich /oxygen- - 41 - deficient condition. However, by increasing the fuel-jet momentum flux and /or by increasing the excess air level, a much higher proportion of the oxygen required for combustion could be supplied through, the entrainment of product gases. CONCLUSIONS Emissions Performance The burner described in the present invention results in ultra low emissions of NOx when operated with preheated oxidant. The burner implements two NOx control mechanisms: high degree of internal flue gas recirculation coupled with a fuel rich reducing zone which converts in part the NOx produced to molecular nitrogen. The reduction in NOx is realized without a penalty in terms of high CO or unbumed hydrocarbons. Burner Variables The effects of the air and exhaust-gas temperatures on NOx are monotonic; the emission rises with increasing temperature. The effects of the burner variables that were studied, namely the fuel-port angle βj and the air port diameter D 2 , should be expected to, and evidently do, show minima. The minima appeared to be fairly flat, giving a fairly broad practical optimum operating region. The NOx levels found for β t = 35° and 42.5° are practically the same. It appears that decreasing ^ l to 30° raises the emission slightly, as does an increase to 65°. Changing the air port diameter D 2 at any given flow rate changes the air jet momentum flux. The NOx levels found for D 2 = 15.88 mm and 19.05 mm are practically the same, but there is a significant elevation at 24.31 mm. It must also be noted that the fuel port diameter Di and the air port angle β 2 were not varied, so the picture afforded by the investigations to date is incomplete. It will be evident, however, from the modelling of the entrainment aerodynamics, that the effect on NOx emissions of the magnitude of the angles is interrelated with the mass and momentum flux ratios, and that negative effects of the former can be counteracted by adjustments of the latter (and vice versa). Although the influence of the fuel jet angle βj on NOx emission is not great over the range studied, the effects on flame definition and combustion stability are of a different magnitude. The relation is monotonic: stability decreases with increasing βj. At β ! = 65°, as may be appreciated from the strong-jet /weak-jet model, the fuel jets are not entrained by the air jets before impinging on the furnace walls. Instead, the fuel jets impinge fully upon the combustion chamber boundaries in the tunnel-furnace operation and from there disperse widely, mixing with the furnace gases. A very dilute fuel - product mixture is then entrained by the air jets. Reaction generally is enfeebled by the dilution and drop in temperature and the effect of reaction zone which is greatly enlarged. Therefore, stability is adversely affected. The turn down limit is considerably raised compared to that at a lower β t and the furnace must be run at higher exhaust gas temperatures to maintain a stable operation. Therefore, larger values of βj are less desirable. Stability improves steadily with decreasing β ly as might be expected from the SJWJ model. The fuel jet ceases to impinge on the furnace walls, arching sufficiently to meet the air jets, and the height and length of the arch decrease. The amount of product gas entrained by both fuel and air jets before they meet decreases. All this improves stability, but at some point fuel and air meet too directly and the NOx production begins to rise. Therefore.the optimum value for β j would appear to be a compromise between a larger value to provide greater NOx reduction and a smaller value to maintain combustion stability. Flame Size and Combustion Intensity The flame size with present burner was found to be somewhat larger than conventional flames, with the intensity being around 60,000 Btu/ft3hr as compared with typical flame intensities of around .150,000 Btu/ft3hr for turbulent diffusion flames. Flame probing, however has demonstrated a stable flame core as opposed to very low intensity volumetric combustion. Moreover it is known that by adjusting angles of introduction of fuel and oxidant jets (β 2 and βi) the flame intensity can be further raised and the flame size reduced. Effect of Auxiliary Burner Continuous operation of the auxiliary burner can improve stability, without apparent penalty in terms of NOx emissions, allowing greater turn down and operation at lower furnace temperature levels. The achievement of low NOx at high air preheat temperature through the principle described in this invention, involves heavy, aerodynamically-induced dilution of air and fuel with cooled products. This mixing results in poor combustion stability. Negative effects of this mixing can be considerably ameliorated by continuous operation of the auxiliary burner. Since a pilot burner must be provided for start-up, additional costs through continuous use of the pilot burner as an auxiliary burner during operation of the burner should be minimal. However, at least for some configurations, temperatures, and /or operating conditions, it may not be necessary to operate the auxiliary burner continuously. Combustion Stability and Operating Temperature Niche Operation at temperatures at below an exhaust gas temperature of 900°C and average of refractory temperature below 830°C can result in flame instability. Therefore, it is considered that steady state levels with the exhaust temperature greater than 1000°C or the refractory temperature greater than 900°C are desirable. Ef feet of 02 Content The burner was operated at a range of excess air levels from fuel rich (negative excess air minus 1.4%) to around 30% excess air under varying furnace operating temperatures. The flame was stable at excess air levels of 10% or more under all furnace operating temperatures. At exhaust temperature levels equal to or higher than 1300°C, stable flame was maintained down to stoichiometric conditions (0% excess air). Even higher exhaust gas temperatures allowed stable operation under fuel rich conditions. At lower exhaust gas temperature levels, a loss of flame was recorded as excess air levels were reduced. However, this is thought to be a flame detection issue, involving the location of the uv flame sensor, rather than an indication of reduction in stability. A mild dependence of NOx emission on excess air was observed. Exhaust gas NOx level was roughly proportional to [1+ 0.4[O 2 ] 1 / 2 ], where 0 2 is the exhaust gas oxygen content on a percent dry basis. Effect of Fuel/Air Momentum Flux Ratio As demonstrated by the strong jet model, the height and the length of the fuel jet trajectories to the point of confluence with the air jets depends on the fuel /air momentum flux ratio, as well as the fuel jet angle. Both height and length are decreased by increasing the fuel port diameter di, thus decreasing the fuel momentum at a given rate. Capacity Rating and Turn Down It appears that for a given burner operating at given levels of excess air and furnace gas temperature, there is a more or less definite lower stability limit, a firing rate below which combustion stability is uncertain and flameouts can be expected. On the other hand, firing rates high enough to produce a high flow instability have - * - -,,„ . - PCT/CA96/00334 - 45 - not been observed, and it appears from theoretical considerations that the flame should be stable at the highest gas and air port velocity that might be of practical interest. The minimum practical firing rate is determined by the low - fire combustion stability of the burner flame in the furnace. The maximum firing rate is normally set by the fan or blower capacity, and an up delivery pressure must be available to counter the pressure drops across the burner, the recuperator (if any), the orifice or other flow - measuring device and the supply line. The maximum turn down (the ratio of the maximum firing rate to the minimum) is apparatus - dependant, the maximum firing rate being determined by the fan or blower capacity. Scale Up Potential Based on data to date, there is no perceived problem in scaling up the burner of the present invention to much larger capacities. The burner has been successfully scaled up from 65kW to 400kW and further scale-up to large industrial sizes is contemplated. Either direct scale-up maintaining geometric similarity, or a non- linear scale-up increasing the number of fuel and oxidant ports, or a combination of these, as was used to scale-up from 65 kW to 400 kW may be adopted for further scale-up. Final Summary It will be recognized that the combination of the number of jets, fuel and air, the angles of orientation of the air and fuel orifices, and the port diameter to be used for any given application depends upon the desired flame characteristics, the nominal input required and the required turn down ratio for a stable flame. The fundamental feature of the present invention is the diverging turbulent jets of air and fuel. It will be understood that a number of different combination of angles can be used so long as the air jets and gas jets diverge. However, optimal NOx reduction may 96/37734 „,--_,.,, PCT/CA96/00334 - 46 - occur at a specific combination, or over a limited range, for a given input and specified flame characteristics. The relation between β j and β 2 must be such that the appropriate aerodynamic entrainment of the air jets .and the fuel jets occurs. Aerodynamic theory of turbulent jet entrainment predicts that if the angles between two divergent jets reaches more than approximately 50°- 60°, entrainment will not occur within a practically reasonable distance and at larger angles the jets will continue to diverge. The relative sizes of the jets are also important. The sizes of the jets must be such that a stable flame is formed. The fuel and air jets must also have sufficient and appropriate relative momentum for entrainment to occur. Momentum of the jets depends on the exit port diameters, the number of jets and the input rate. There are other design limits arising from physical constraints for a given firing rate and size of burner head. Given a set of required operating conditions, it can be predicted with reasonable accuracy and a minimum amount of routine experimentation what the optimal configuration should be. As a result of the observations described above, it is believed that the number of air jets and fuel jets could range from 3 to 30, the upper limit subject to physical constraints such as space to provide the jets and input rate. It is also believed that the angle of the air jets can vary from 0° to 30° and the angle of the fuel jets can range from 10° to 70°. It will be understood that the choice of the two angles is interrelated, subject to the discussion above. While the above description constitutes the preferred embodiments, it will be appreciated that the present invention is susceptible to modification and change without parting from the fair meaning or proper scope of the accompanying claims.

Claims: WE CLAIM: 1. A burner, for combusting a gaseous fuel, the burner comprising: an oxidant supply duct; a fuel supply duct; an oxidant orifice means connected to the oxidant supply duct, for discharging at least one oxidant jet; a fuel orifice means connected to the fuel supply duct, for discharging at least one fuel jet; wherein the oxidant orifice means and the fuel orifice means are arranged such that the oxidant and fuel jets diverge from one another, the divergence being such that the oxidant or fuel jets entrain a substantial quantity of surrounding furnace gases to effect recirculation of the furnace gases and such that the oxidant and fuel jets eventually entrain and mix with one another to form a stable combustion zone, wherein the entrainment of furnace gases effects dilution of the oxidant and the fuel in the combustion zone, thereby lowing temperatures in the combustion zone and wherein the fuel jets undergo pyrolysis during the course of their trajectories creating a reducing zone. 2. A burner as claimed in claim 1, which includes a longitudinal axis, wherein at least one orifice means, of the oxidant orifice means and the fuel orifice means, extends along the longitudinal axis, wherein the other orifice means, of the oxidant orifice means in the fuel orifice means, encircles said one orifice means. 3. A burner as claimed in claim 2, wherein said other orifice means comprises a plurality of orifices arranged to form jets diverging away from the longitudinal axis. - 48 - 4. A burner as claimed in claim 3, wherein the oxidant orifice means comprises said one orifice means and comprises a plurality of oxidant orifices arranged generally symmetrically around the longitudinal axis of the burner, and wherein the fuel orifices means comprises said other orifice means and comprises a plurality of fuel orifices encircling the oxidant orifices and arranged generally symmetrically around the longitudinal axis of the burner; 5. A burner as claimed in claim 4, wherein the oxidant orifices are provided in a first circle around the longitudinal axis and evenly spaced along the periphery of the circle, wherein the fuel orifices are arranged in a second circle and are evenly spaced along the periphery of the second circle, and wherein the oxidant orifices are inclined at a first angle to the longitudinal axis and the fuel orifices are inclined at a second angle to the longitudinal axis greater than the first angle. 6. A burner as claimed in claim 5, wherein the fuel and oxidant orifices are provided in a common housing and wherein the oxidant and fuel supply ducts extend separately into the housing. 7. A burner as claimed in claim 6, wherein an equal number of oxidant orifices and fuel orifices are provided. 8. A burner as claimed in claim 7, wherein each of said fuel orifices is spaced equally between two adjacent oxidant orifices. 9. A burner as claimed in claim 8, wherein the number of oxidant orifices ranges from 3 to 30. 10. A burner as claimed in claim 7, wherein the angle of the longitudinal axis of the oxidant orifices ranges from 0 to 30 degrees. 11. A burner as claimed in claim 7, wherein the second angle of the fuel orifices ranges from 10 to 70 degrees. 12. . A burner as claimed in claim 7, wherein 6 oxidant orifices are provided, said first angle of the oxidant orifices is 10 degrees, and said second angle of the fuel orifices is 65 degrees. 13. A burner as claimed in claim 7, wherein 7 oxidant orifices are provided, said first angle of the oxidant orifices is 10 degrees, and said second angle of the fuel orifices is 65 degrees. 14. A burner as claimed in claim 3, wherein 7 oxidant orifices are provided, said first angle of the oxidant orifices is 10 degrees, and said second angle of the fuel orifices is 35 degrees. 15. A burner as claimed in claim 1 further comprising an auxiliary burner for ignition from a cold start and for constant operation during combustion, the auxiliary burner comprising a housing, a spark electrode, an inlet for gas, and an inlet for oxidant, so that when oxidant and fuel are introduced into said housing through said inlets, and said electrode is sparked, combustion of the introduced fuel and oxidant creates a pilot flame. 16. A burner as claimed in claim 6, wherein the housing includes a burner block comprising a ceramic of a grade to withstand high temperature. 17. A method of combusting a gaseous oxidant and a gaseous fuel, the method comprising: discharging the oxidant in at least one discrete jet; simultaneously discharging the fuel in at least one discrete jet; adjacent jets of fuel and oxidant being arranged to diverge away from one another such that at least one of the oxidant jet and the fuel jet entrain a substantial quantity of surrounding furnace gases to effect recirculation of the furnace gases, and such that the oxidant and fuel jets eventually entrain and mix with one another to form a stable combustion zone, the entrained furnace gases effecting dilution of the oxidant and the fuel in the combustion zone to lower temperatures in the combustion zone and wherein the fuel jets undergo pyrolysis during the course of their trajectories creating a reducing zone. 18. A method as claimed in claim 17, wherein a plurality of jets of oxidant and a plurality of jets of fuel are provided, wherein one of the oxidant and the fuel jets encircles the other of the oxidant and fuel jets. 19. A method as claimed in claim 18, wherein the oxidant jets are provided generally symmetrically arranged in a circle, and wherein fuel jets are generally symmetrically arranged in another circle, encircling the oxidant jets. 20. A method as claimed in claim 19, wherein the oxidant and fuel jets have approximately similar jet velocities. 21. A method as claimed in claim 19, wherein the momentum flux ratio of the fuel jets to the oxidant jets is in the range 0.005 - 0.08. 22. A method as claimed in claim 19, wherein there are an equal number of oxidant jets and fuel jets, which alternate with one another, wherein the jets are arranged around a longitudinal axis with - 51 - the oxidant orifices inclined from the longitudinal axis by an angle in the range 0° - 30° and the fuel jets inclined from the longitudinal axis by an angle in the range 10° - 70°.

Inventors: BECKER HENRY A, BESIK FERDINAND K, RAHBAR SHAHRZAD, SOBIESIAK ANDRZEJ, BECKER, HENRY, A., BESIK, FERDINAND, K., RAHBAR, SHAHRZAD, SOBIESIAK, ANDRZEJ
Applicants: CANADIAN GAS RESEARCH INST, CANADIAN GAS RESEARCH INSTITUTE
Application year: 1996
Main classification: F23C9
IPC codes: F23C9, F23D14, F23D23