US3868211A - Pollutant reduction with selective gas stack recirculation - Google Patents

Pollutant reduction with selective gas stack recirculation Download PDF

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Publication number
US3868211A
US3868211A US432623A US43262374A US3868211A US 3868211 A US3868211 A US 3868211A US 432623 A US432623 A US 432623A US 43262374 A US43262374 A US 43262374A US 3868211 A US3868211 A US 3868211A
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Prior art keywords
fuel
combustion
air
carbon dioxide
gas
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US432623A
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Paul G La Haye
John W Bjerklie
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Aqua Chem Inc
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Aqua Chem Inc
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Priority to US432623A priority Critical patent/US3868211A/en
Priority to GB5093174A priority patent/GB1464169A/en
Priority to CA214,788A priority patent/CA1042339A/en
Priority to NL7415901A priority patent/NL7415901A/xx
Priority to ZA00747776A priority patent/ZA747776B/xx
Priority to FR7441278A priority patent/FR2257861B1/fr
Priority to BE151467A priority patent/BE823312A/xx
Priority to DE2461078A priority patent/DE2461078C2/de
Priority to CH1729274A priority patent/CH592846A5/xx
Priority to JP50003022A priority patent/JPS50102933A/ja
Priority to IT31028/74A priority patent/IT1028056B/it
Priority to ES433324A priority patent/ES433324A1/es
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Publication of US3868211A publication Critical patent/US3868211A/en
Assigned to WALTER E. HELLER & COMPANY, INC., A CORP. OF DE reassignment WALTER E. HELLER & COMPANY, INC., A CORP. OF DE SECURITY INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: HAGUE INTERNATIONAL
Priority to JP1982058584U priority patent/JPS58111U/ja
Assigned to AQUA-CHEM HOLDING, INC., A CORP. OF DE reassignment AQUA-CHEM HOLDING, INC., A CORP. OF DE ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: AQUA-CHEM, INC. A DE CORP.
Assigned to AQUA-CHEM, INC. reassignment AQUA-CHEM, INC. CHANGE OF NAME (SEE DOCUMENT FOR DETAILS). EFFECTIVE JAN. 18, 1982. Assignors: AQUA-CHEM HOLDING, INC.
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C9/00—Combustion apparatus characterised by arrangements for returning combustion products or flue gases to the combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C6/00—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion
    • F23C6/04—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion in series connection
    • F23C6/045—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion in series connection with staged combustion in a single enclosure
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2201/00—Staged combustion
    • F23C2201/20—Burner staging
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2202/00—Fluegas recirculation
    • F23C2202/10—Premixing fluegas with fuel and combustion air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2900/00—Special features of, or arrangements for combustion apparatus using fluid fuels or solid fuels suspended in air; Combustion processes therefor
    • F23C2900/06041—Staged supply of oxidant

Definitions

  • a recently made important improvement in reducing the aforementioned pollutants is characterized as radially staged combustion which involves injecting fuel into a combustion chamber with less than the amount of air required for stoichiometric combustion so that burning takes place in a flame core which has a relatively small diameter near the burner and expands outwardly as it is propagated down the combustion chamber.
  • the core mixture is rich in fuel, combustion is very incomplete near the burner and the gaseous core is much cooler than it would be if all the air for complete combustion were injected in the fuel.
  • the cooler temperatures and rich fuel content of the core tends to inhibit formation of nitrogen oxides. This results in part from the oxygen in the air combining preferentially with the constituents of the fuel instead of with nitrogen under low temperature fuel-rich conditions.
  • a sheath of air is also injected so as to surround and swirl around the core with little mixing near the burner. After some heat is extracted from the core as it progresses down the combustion chamber, mixing of the core gases and sheath air becomes more complete and the unburned constituents are oxidized in this stage under relatively low temperature conditions again so as to inhibit nitrogen oxide production.
  • further mixing turbulence is promoted by a grid interposed in the flame path remote from the burner.
  • Some of the combustion air may also be injected through, the grid to increase velocity and promote turbulence which encourages oxidation of the combustible constituents without significant production of nitrogen oxides since intimate mixing rather than high temperature is relied upon to complete oxidation.
  • the arrangement just discussed is effective in reducing unburned solids such as carbon and nitrogen oxide.
  • the stack gases have a higher than desired amount of carbon manifested as smoke.
  • the present invention is concerned with reducing smoke as well as nitrogen oxides and other pollutants in the stack gases by a method which is applicable to the above described staged combustion technique and other fuel burning techniques as well by the selective recirculation of stack gas.
  • a general object of this invention is to provide a combustion method and apparatus wherein nitrogen oxides, carbon monoxide, gaseous and particulate hydrocarbons and carbon in the exhaust or stack gas are substantially reduced as compared with conventional methods wherein all of the combustion supporting gases are introduced intimately with the fuel.
  • Another object is to react carbon dioxide from the exhaust gases with carbon resulting from incomplete combustion and to react the resulting combustion products with oxygen from air to reduce carbon and carbon monoxide in the exhaust gases.
  • a further object of this invention is to provide a combustion method and apparatus for minimizing the aforementioned atmospheric pollutants without adversely affecting the efficiency of the combustion process by selectively recirculating the stack gases and thereby reducing to a minimum the amount that must be recirculated to accomplish a given result.
  • Another object of this invention is to minimize in the exhaust gases from a fuel burner the particulate carbon content which appears as smoke and yet maintain satisfactorily low levels of nitrogen oxides in the stack gases.
  • FIG. 1 shows a boiler with parts broken away to illustrate a combustion device in which the principles of the invention are used;
  • FIG. 2 shows a fragmentary cross section of a combustion chamber and an associated burner adapted for stack gas recirculation in accordance with the invention
  • FIG. 3 is similar to the preceding figure except that a different kind of burner arrangement is shown;
  • FIG. 4 is a fragmentary longitudinal section of a combustion chamber adapted for use of recirculted stack gases
  • FIG. 5 is a plan view of an aperture plate used in the burner assemblies of FIGS. 2 and 3 as specifically exemplified by viewing in the direction of the plane 5-5 in FIG. 2;
  • FIG. 6 is a graph showing burning time versus carbon particle size for various percentages of combustion supporting carbon dioxide and air.
  • the invention is based on recirculating exhaust gases boiler in FIG. 1 is substantially conventional.
  • This boiler is for producing hot water or steam and includes a shell or housing constituting an enclosure for an upper drum 11 and a lower drum 12.
  • the drums are connected by means of a plurality of water filled tubes 13 on the foreground side and another plurality of tubes, not visible, on the background side.
  • the tubes have membranes or web plates 14 welded between them to define a cavity in which heat is derived by the tubes from hot combustion gases discharged from a combustion chamber and by radiation from the combustion chamber.
  • the exhaust gases after most of their heat is extracted, are discharged to the atmosphere through a stack 15 which is shown fragmentarily.
  • the front end, to the right in FIG. 1, of the boiler has an air plenum l6 and a recirculated stack gas plenum 17.
  • the stack gas plenum 17 is supplied with stack gas through a pipe 18 which junctions with the stack pipe 15 near the top of the boiler' housing so that gas at temperatures at least in the range of 60C to 400C will be available from the stack.
  • Stack gas pipe 18 may have a valve 19 installed in it which valve in this case is merely symbolizedas a manual one but it will be understood that it may be subject to automatic throttling.
  • a low pressure blower 20 may be used under some circumstances to force the stack gases from the stack 15 to plenum 17.
  • Air plenum 16 has an internal fan blade 20 driven by a motor 21. This fan draws atmospheric air through a grille 22 and directs the air downwardly in plenum 16 for introduction through one or more air injection ports associated with a fuel burner which is generally designated by the numeral 23 in FIG. 1. The fuel burner will be described in detail later.
  • the combustion chamber of the boiler comprises a refractory housing 25 having a cylindrical interior 26.
  • the combustion -chamber 25 need not be'of the refractory lined type but may be simply defined by the boiler tubes or may be a water jacket type having inner and outer shells, not shown, between which water flows for directly absorbing heat by radiation and convection from the flame within the combustion chamber.
  • the fuel and combustion gas inlet end of combustion chamber 25 preferably has a conical shape marked 27 although this is not indispensible insofar as application of the principles of the invention are concerned.
  • Combustion chamber 25 is characterized by combusting the gases and fuel in stages in this example.
  • the fuel is injected into combustion chamber 25 along with air or stack gases or a mixture thereof.
  • the fluid fuel being injected with much less air than is required for complete combustion, burns as a central core of flame which is indicated by the centrally heavily shaded region in FIG. 1 marked with the numeral 28.
  • the shortage of air for complete combustion in core 28 results in a relatively low temperature core flame near burner 23 where the core has not undergone significant turbulence that would result in its expansion and diffusion with air or other combustion supporting gas in the chamber.
  • a characteristic resulting from isolation of the sheath air 29 from the hotter gaseous combustion products in core 28 is that the oxygen which is available from the air in the core has a tendency to combine with the hydrocarbons from the fuel in preference to nitrogen from the air in which case substantial amounts of carbon monoxide and some carbon dioxide are produced but relatively low amounts of the various nitrogen oxides are produced. There is also substantial unburned carbon in the flame core at this time. Low production of nitrogen oxide results from the fuel rich mixture in the core 28 burning at a temperature sufficiently below 1,375C that the reaction betweennitrogen and oxygen is inhibited.
  • the present invention is concerned with obtaining more complete combustion of the carbon without sacrificing the good nitrogen oxides inhibiting characteristics of the staged combustion process.
  • stack gases are recirculated to the burner chamber and these gases are primarily injected into the flame core 28 to obtain smoke control.
  • the good results obtained in reducing smoke emitted by stack 15 are believed to be due to the reaction of C0 (carbon dioxide) in the recirculated stack gases with the fine carbon particles in the flame core before and after diffusion to thereby form CO (carbon monoxide) which, according to the invention, is caused to burn cleanly later to CO
  • CO carbon monoxide
  • Carbon particles in smoke resulting from burning hydrocarbon fuels in gaseous form are usually about 0.05 microns in size.
  • Carbon particles resulting from burning liquid hydrocarbon fuel are usually in the size range of l to microns and some particles are formed within droplets of fuel.
  • the relationship between the burning time in milliseconds and carbon particle size in the presence of 25, 50 and 100 percent CO and in the presence of air for carbon particles ranging from .01 to 10.0 microns is shown graphically in FIG. 6. The burning times are calculated and are based on the following equation:
  • k is an empirical combustion rate constant peculiar to each fuel and burning condition.
  • Carbon burning in air or CO reaches a maximum combustion rate in the range of l,200 to l,400C. At 1,300C the rate is nearly maximum. Above these temperatures, the rate appears to remain substantially constant.
  • FIG. 2 which shows one type of burner assembly 23 associated with a combustion chamber 25 similar to the one depicted in FIG. 1.
  • the burner assembly 23 associated with a combustion chamber 25 similar to the one depicted in FIG. 1.
  • burner comprises a nozzle body 36 having a tip 35 from which a mixture of fuel and an atomizing gas such as high pressure air is emitted for the purpose of combustion in combustion chamber 25.
  • the nozzle tip 35 is supplied with fluid fuel through a pipe 37 and the atomizing or vaporizing substance through a pipe 38.
  • Adjacent to nozzle tip 35 is a hollow cylinder or sleeve 39 through which the fuel is projected into combustion chamber 25 where it burns.
  • Sleeve 39 may be omitted without seriously affecting smoke when No. 2 fuel oil is used although flame color changes from blue to yellow.
  • Sleeve 39 is omitted when using No. 2 fuel to prevent the accretion.
  • These combustion supporting gases are admitted through a diaphragm 40 having an aperture 41.
  • the gases are proportioned as will be explained.
  • Diaphragm 40 extends across a hollow cylinder 42 which surrounds a portion of the nozzle body and is spaced in essentially concentric relationship with sleeve 39.
  • the rear interior portion 43 of hollow cylinder 42 is arranged for enabling conducting air, stack gas containing CO and mixtures of these gases as desired to aperture 41.
  • air flow is normally so regulated that much less than the stoichiometric quantity of air is supplied to the core flame 28 to thereby inhibit production of nitrogen oxides.
  • the amount of recirculated CO containing stack gas is so controlled as to promote oxidation or burning of carbon in the core 28 independently of the air of combustion.
  • CO is introduced into the core flame 28 by recirculation of stack gas for reaction with carbon in the core flame which results in production of carbon monoxide in quantities significantly greater than would occur if all of the air for combustion of the fuel were mixed with the fuel according to conventional practice.
  • Some carbon dioxide containing combustion gases also recirculate into the core as a result of a venturi effect which occurs in the vicinity of aperture 41 and the mouth 44 of sleeve 39.
  • the burner assembly 23 which is symbolically depicted in FIG. 2 has a hollow region 43 upstream for enabling directing air or stack gas or both through aperture 41.
  • I-Iollow region 43 communicates with another chamber 45 which is surrounded by the stack gas plenum 17.
  • Chamber 45 may be cylindrical and provided with a plurality of holes 46 which can be aligned and misaligned with a similar plurality of holes 47 in a rotatable sleeve 48. Since the holes 46 and 47 are circumferentially spaced from each other, it is possible to rotate sleeve 48 in such manner as to completely align holes 46 and 47 or misalign them to regulate the stack gas that can enter region 43. This permits control or throttling of the amount of carbon dioxide containing stack gas which is admitted to flame core 28.
  • a selected amount of combustion air may also be admitted to flow out through aperture 41 for supporting combustion in the core 28 of fuel injected from nozzle tip 35.
  • cylinder 42 is provided with a plurality of circumferentially spaced holes 51 which are surrounded by a sleeve 52 in which there are also a plurality of circumferentially spaced radial holes 53.
  • Sleeve 52 may be rotated to adjust the quantity of air that is admitted to aperture 42 for supporting combustion in the core flame 28.
  • Air is obtainable from a pressurized plenum 16 in which there also may be a control damper 55 that can grossly regulate the amount of air provided by fan 20 in the plenum.
  • Air from plenum l6 flows into a cavity 56 through a plurality of holes 57 in the burner housing wall which can be made to align or misalign with a plurality of holes 58 in a rotatable sleeve 59 for regulating air input.
  • a radial flange 60 extending from cylinder 42 together with a perforated aperture plate 61 defines air cavity 56.
  • much of the air needed for complete combustion of the fuel is supplied to the combustion zone through a plurality of perforations 62 in the plate 61.
  • a plan view of the plate is shown in FIG. 5 where it can be seen that it has a plurality of apertures 62 which may be formed by piercing the parent metal so as to produce angularly and axially extending vanes 63 which cause air projected through the apertures to be deflected radially of the flame core 28 and to form a helically advancing sheath about it.
  • any suitable means may be substituted for the specific perforated plate 61 to produce the slowly rotating sheath of air which follows along flame core 28 and surrounds it through most of the combustion zone until mixing eventually occurs.
  • the component of rotation may be such as to approach or reach zero.
  • the air flowing through the aperture plates 61 and the core flame remain fairly well isolated and can be called a sheath, but as the flame is propagated down the combustion zone there is significant mixing of the air and core, after heat has been extracted from the latter, to effectuate combustion of unburned components at a temperature which inhibits production of nitrogen oxides.
  • the carbon dioxide from the stack gases reacts with carbon present in the combustion zones to produce substantial carbon monoxide which is ultimately oxidized to carbon dioxide before it is returned to the stack as will be explained.
  • stack gas may be injected through the apertured plate ,61 by suitably balancing the air pressure and stack gas pressure in their respective plenums l6 and 17.
  • air or air and CO containing exhaust gases in sheath 29 progresses down the combustion chamber away from the burner, and as the CO rich core 28 expands in the same zone, some turbulence and intermixing occurs which promotes combustion of residual combustion products.
  • the temperature required for the maximum reaction of CO and carbon to produce C are over 1,250 C so production of CO is relatively high.
  • the perforations 72 in the screen means result in a gas velocity increase from the combustion chamber side to the discharge side and this promotes the turbulence external to the chamber which results in more complete oxidation of the carbon monoxide and any other combustion products that may remain in the combustion gases.
  • a grid means that produces a pressure drop of about 0.3 percent of the furnace upstream pressure just beyond cone 27 or 2 inches of water pressure for boiler furnaces operating 8 v at essentially atmospheric pressure will produce the necessary turbulence and intermixing.
  • a plurality of parallel pipes 64 are interposed across the gaseous combustion product stream for inducing mixing of the gases.
  • the spacing between the pipes 64 is such that the pressure drop approximating that mentioned above is produced.
  • the parallel pipes 64 in FIG. 2 may be connected to a header 65 which received a supply of air through a pipe 66 from the air plenum 16, for instance.
  • the pipes 64 When the pipes 64 are used to inject air rather than merely as a means for producing a pressure drop, they are provided with rows of small holes 67 on the downstream side or at the sides. Air is emitted from the holes for the purpose of completing the oxidation of carbon monoxide and other residual burnable products.
  • the combustion chamber may be provided with a second set of perforated pipes 68 connected to another header 69 which receives an air supply through an input pipe 70.
  • the amount of air fed through the second pipe 70 is usually less than that which is supplied through the first supply pipe 66 since usually a sufficient quantity of air is emitted from pipes 68 for completing oxidation of only small quantities of incompletely oxidized combustible substances.
  • Secondary air for burning carbon or other combustibles under turbulent conditions and at comparatively low temperature remote from the burner may also be introduced through orifices 73 in the combustion chamber 25 wall as shown in FIG. 4.
  • the orifices may be supplied from a header 74 which is connected to the air plenum 16 by suitable pipe means, not shown.
  • the new method involving recirculation of CO containing stack gas may be practiced with various types of fluid fuel burners.
  • the burner just described in connection with FIG. 2 is especially well adapted to burn-' ing highly volatile fuels such as No. 2 fuel oil for obtaining low carbon particulates, CO and nitrogen oxides by properly proportioning recirculated exhaust gases and air for combustion through apertured plate 61 and the air injecting grids 64 and 68 or, in some cases, by merely producing turbulence with a pressure drop through a grid.
  • Other burner configurations are more appropriate for reducing carbon and nitrogen oxides in the exhaust gases when less volatile fuels such as No. 6 fuel oil is used. Practicing the new stack gas recirculation method under these circumstances will now be discussed in reference to FIG. 3. I
  • the burner assembly is generally designated by the reference numeral 80. It comprises an inner hollow cylinder 81 across which fuel and combustion air and carbon dioxide containing exhaust gas may be projected into combustion chamber 25
  • the exterior of cylinder 81 is surrounded by an input gas distributor or aperture plate 84 having a plurality of perforations 85 for projecting air about the periphery of the flame core 86 which, in this case as in the previous case, comprises a mixture that is low in combustion air content and rich in fuel so that it burns at relatively low temperature and thereby inhibits nitrogen oxides production.
  • Aperture plate 85 together with a flange 87 which extends radially frorn the rear end of cylinder 81 defines an air cavity 88.
  • Cavity 88 has two exits for air, the first being into the combustion chamber 25 through the perforations 85 in plate 84 and the second being to the interior of cylinder 81 through holes 89 in a rotatable damper ring 90.
  • Holes 89 line up with a plurality of holes 91 in cylinder 81 and, as in the previously discussed example, damper ring 90 may be rotated to vary the alignment between holes 89 and 91 and thereby regulate air flow through them to the interior of cylinder 81.
  • Air is supplied to cavity 88 from a plenum 92 which is pressurized by a motor driven fan or blower blade such as 20 in FIG. 1. Air flow from plenum 92 to cavity 88 is regulated by selective rotation of a damper ring 93 so that its apertures 94 may be selectively aligned with a plurality of holes 95 in a stationary ring 96.
  • the burner in FIG. 3 includes a substantially conventional burner nozzle assembly 97 which is supplied with fluid fuel through a fragmentarily shown inlet pipe 98.
  • a suitable gas such as air for atomizing the burner fuel may be admitted through a pipe 99.
  • an atomizing gas need not be used and the fuel may be atomized by merely forcing it through small orifices, not shown, in the nozzle 97 tip.
  • Recirculated stack gas may be injected through aperture 83 in surrounding relation to the atomized fuel from a cavity 100 which communicates with a stack gas plenum marked 17' in FIG. 3.
  • the flow of stack gas from plenum 17 to cavity 100 and thence through gas and fuel exit aperture 83 is again regulated by a symbolically shown rotatable ring 101 which has a plurality of apertures 102 that are subject to varying degrees of alignment with apertures 103 in a stationary shell 104.
  • Stack gases may be admitted under pressure to plenum 17 from a pipe 18' which communicates with stack 15 as suggested in FIG. 1.
  • combustion is carried on in stages as in the previously discussed embodiment.
  • Relatively low temperature combustion occurs in the fuel rich flame core 86, particularly adjacent the exit of the burner.
  • Some of the combustion air is admitted to combustion chamber 25' in surrounding relation to core 86 by means of apertures 85 in plate 84.
  • This air advances in a long pitch helix longitudinally of the combustion chamber 25 or it may simply advance longitudinally or axially to ultimately undergo mixing with the gases in core 86.
  • Combustion is incomplete in the core 86 and considerable smoke particles and C are produced. Since some heat is extracted from core 86 by means of radiation and convection, final combustion takes place in the mixing zone remote from the burner at low enough temperatures so that significant nitrogen oxides are not produced.
  • the carbon dioxide available from the exhaust gases which are injected into the core flame 86 react with the carbon particles in the core along the way and near the final mixing zone and produce high levels of carbon monoxide and some particulate carbon in the first stage of the combustion chamber but, later on, when turbulence and mixing become more complete, oxygen from the surrounding sheath air or air that is introduced by the other means reacts with the carbon monoxide and reconverts it to carbon dioxide before the gaseous combustion products exit to the stack 15. Carbon particles remaining are also consumed at this point. Again, this reaction is at such low temperatures that little nitrogen oxides are produced.
  • FIG. 3 depicted in FIG. 3 and generally designated by the numeral 106.
  • the grid comprises a plurality of pipes 107 which are spaced apart from each other by a sufficient distance to produce a pressure drop across the grid.
  • a drop of about 0.3 percent of the furnace pressure is usually satisfactory but it may be slightly less or even higher such as up to 10 percent of the furnace pressure.
  • the grid 106 may also comprise pipes 107 with a plurality of perforations directed downstream or cross stream for injecting combustion air to completely oxidize residual unburned products.
  • Pipes 107 may be connected to a transversely extending header 108 which is supplied with oxygen containing gas through a pipe 109 that may be connected back to the air plenum 92 or other suitable source of combustion supporting gas, not shown.
  • the grid 106 in FIG. 3 and its counterparts in FIG. 2 may simply consist of water or flue gas tubes which are part of the boiler or other heat exchange components as long as the pipes are near the exit of the combustio'n chamber 25 and are sufficiently closely spaced to produce some pressure drop and, hence, turbulence and mixing of the gases.
  • the back wall of the combustion chamber downstream may become hot enough to maintain ignition of the gaseous mixture to thereby result in oxidizing any residual carbon or carbon monoxide to carbon dioxide provided adequate air is available.
  • complete burnout of the gaseous and particulate combustibles can be obtained where the backwall temperature exceeds 982C and the pressure drop from the combustion chamber into the boiler tube region is adequate to assure complete mixing.
  • the proportions of sheath air and recirculated stack gas differ as between different burners and fuels as has been suggested.
  • the relative amount of air admitted in the core and through the aperture plates such as plates 61 and can vary from nearly all of the air going through the plates to over half of it going directly into 'the core with the atomized fuel.
  • as little as 40 percent of the air total or stoichiometric combustion was admitted through the aperture plate and to the core with the rest issuing from the grids 106.
  • the recirculated stack gas flow equaled the core plus the aperture plate air flow.
  • the new method involves recirculating stack gases into the fuel rich core along with a small amount of air and all the fuel as a means of controlling nitrogen oxidesand smoke simultaneously.
  • Some additional control over nitrogen oxides produced is obtained for higher volatility fuels by properly dividing the secondary air between the first grid 64 and the second grid 68 as in FIG. 2.
  • the second grid may be dispensed with and only a first grid 106 may normally be required to admit the secondary combustion air.
  • Typical proportions for the various gases involved in the combustion method herein set forth are listed in the following Table I where the quantities under the column headed by FIG. 2 are typical for a high volatility fuel such as would be used in a burner depicted in FIG.
  • FIG. 3 the quantities under the heading FIG. 3 are typical for those which would be applicable to a low volatility fuel such as would preferably be burned in a burner of the type depicted in FIG. 3.
  • the air and recirculated stack gas quantities may have to be adjusted for the particular fuel used to obtain minimum nitrogen oxides and carbon monoxide and unburned hydrocarbons in the stack gases.
  • percent is referred to the total mass flow of the exhaust gases from the combustion system to the atmosphere that is, after subtraction of the recirculated stack gases.
  • a method of burning fuel comprised substantially of hydrocarbons to reduce nitrogen oxides, carbon monoxide, unburned hydrocarbons and carbonaceous particulates in the exhaust gases therefrom, comprising:
  • an ignited core stream comprising a reacting mixture of finely divided fuel, air in an amount substantially less than needed for'stoichiometric combustion of the fuel, and recirculated carbon dioxide containing gaseous combustion products
  • reaction being characterized by the temperature of the gaseous combustion products in said core being lower than would be the case if a substantial portion of the stoichiometric amount of air were included therein so that reaction between oxygen from the air and available nitrogen is suppressed and substantial amounts of carbon are produced, and carbon dioxide reacting with said carbon to produce substantial carbon monoxide, and
  • a method of burning fuel comprised substantially of hydrocarbons to reduce nitrogen oxides, carbon monoxide, unburned hydrocarbons and carbonaceous particulates in the exhaust gases therefrom, comprismg:
  • an ignited core stream comprised of finely divided fuel, air containing gas and carbon dioxide containing externally recirculated stack exhaust gas characterized by at least an upstream region of said core stream having substantially less oxygen than required for complete combustion of the fuel whereby to establish combustion at a sufficiently low temperature in said region to suppress production of nitrogen oxides and produce substantial carbon particulates for reaction with said carbon dioxide to produce substantial amounts of carbon monoxide,
  • the amount of externally recirculated exhaust gas introduced with fuel in the upstream region of said core stream is about to 30 percent the total mass flow of exhaust gases resulting from burning said fuel under the conditions set forth.
  • the amount of air introduced with fuel in the upstream regions of said core stream is in the range of about 5 to percent of the total mass flow of stack discharged exhaust gases resulting from burning said fuel under the conditions set forth.
  • the amount of air introduced in said additional air including gas stream for mixing with said core stream as aforesaid is to 50 percent in terms of stack discharged mass flow of exhaust gases resulting from burning said fuel under the conditions set forth.
  • the amount of air introduced as said first quantity is about from O to 50 percent of the total mass flow of exhaust gases resulting from burning said fuel under the conditions set forth.
  • the amount of air introduced as said second quantity of air is about 0 to 50 percent of the stack discharged mass flow of exhaust gases.
  • the amount of exhaust gases introduced with said fuel in the upstream portion of said core stream is Q91 zi ers nt of t e stea QQ aI s flow of exhaust gases resulting from burning said fuel under the conditions set forth.
  • the amount of said additional air introduced to mix with said core stream downstream is from to percent of the stack discharged mass flow of exhaust gases resulting from burning said fuel under the conditions set forth.
  • the amount of air introduced in said core stream along with said fuel and carbon dioxide containing exhaust gas is about 0 to 10 percent of the total mass flow of exhaust gases resulting from burning said fuel under the conditions set forth.
  • said additional air is introduced as a stream surrounding said core stream and flowing confluently therewith.
  • said exhaust gases are introduced into said core stream at a temperature of to 400C.
  • Apparatus for burning fuel comprised substantially of hydrocarbons to obtain low levels of nitrogen oxides, carbon monoxide and unburned substances in the exhaust gases therefrom, comprising:
  • burner means coupled with said combustion zone defining means, said burner means including means for injecting fuel into said zone and means defining passageways for selectively injecting gases selected from the group of carbon dioxide containing gaseous combustion products and air and mixtures thereof into said zone concurrently with said fuel,
  • At least a first one of said gas passageway defining means being for flowing gas including carbon dioxide from an upstream direction of said injecting means and past said injecting means in surrounding relationship therewith and concurrently with said fuel to effect an ignited core stream for progressing through said combustion zone,
  • a second one of said gas passageways being for introducing at least one of said gases into said combustion zone contiguous with said core-stream for reacting with constituents thereof, and
  • said fuel injecting means comprise nozzle means having orifice means directed to said combustion zone;
  • said first one of said passageway defining means comprising diaphragm means having an aperture aligned with said nozzle means, whereby to direct said combustion supporting gas confluently with saidtue tqe a l sc tatism 0f a r Stream- 21.
  • said fuel injecting means comprise nozzle means having orifice means directed to said combustion zone
  • said first one of said gas passageway defining means including a cylinder means aligned with said nozzle means and arranged relative to said nozzle means such that fuel and gas including said carbon dioxide may flow confluently therethrough into said combustion zone to form said core stream.
  • Apparatus for burning fuel comprised substantially of hydrocarbons to obtain low levels of nitrogen oxides, carbon monoxide and unburned substances in the exhaust gases therefrom,'comprising:
  • Apparatus for burning fuel comprised substancore stream for progressing through said combustion zone,
  • defining means including means for injecting fuel tneans returnmg to a first passageway P9 into said zone and means for defining passageways tion of the gaseous exhaust products containing for selectively injecting gases selected from the Carbon t e resulting r O b fl n
  • 81d group consisting of carbon dioxide containing gase- 10 Zone i eXltmg therefrom, ous combustion products and air and mixtures means interposed gasews combustlfm P thereof into said zone concurrently with said fuel, sffeam near tilt? f 0f a m llS l0 0ne c.
  • definllt'lg means at least a first one of said gas passageway defining definllt'lg means, 5a1d mterPosed means havmg a means being for flowing gas including carbon diox- Pluramy of Pp for safld gases to flow f f g ide concurrently with said fuel to effect an ignited to thereby mcfease Velocity and effect mlxlflg of core stream for progressing through said combusthe gases Core sttream and the 8 tion Zone, cuted to said combustion zone from said second (1.
  • Apparatus for burning fuel comprised substane' means for returning to Said first passageway a pop tially of hydrocarbons to obtain low levels of nitrogen tion of the gaseous exhaust products containing oxides, carbon monoxide and unburned substances ln carbon dioxide resulting from combustion in said the exhaust gases, therefrom )mpnsmg: zone and exiting therefrom a.
  • Injecting fuel means including a cylinder means aligned with said mm Sald p for de mmg paszageways nozzle means and arranged relative to said nozzle for Selectliely m-lectmg gaes.selected.
  • At least a first one of said gas passageway defining h dia hi'a m means transverse to said c linder means bemg for g gasmcludmg Carboy-l dioxfi havin an a erture therein wgich is lde concurrently with said fuel to effect an ignited aligned with said iozzle ineans said aperture ad c-ore Stream for progressing through Said combusi n ne, mltfmg Sald gas fi carbfm dloxlde, to Sam 40 d.
  • a second one of said gas passageways being for incylinder means for exiting to said combustion zone tm-ducing at least one of said gases into Said 23co lr ;1 stream.t t f th I l 19 h bustion zone contiguouswith said core for reacting e mven ion se or in 0 mm W erem: v
  • first grid means comprised of tube means having a means and passageways for regulatmg the amount plurality of oxygen containing gas exit holes, said first grid means being interposed in thegaseousv combustion product stream remotely downstream from said burner means to mix said oxygen containing gas into said stream for burning to carbon dioxide a substantial portion of the carbon monoxide which is produced by the reaction between carbon and carbon dioxide in said core stream.
  • Apparatus for burning fuel comprising substantially hydrocarbons to obtain low levels of nitrogen oxides, carbon monoxide and unburned substances. in the exhaust gases therefrom, comprising:
  • burner means coupled with said combustion zone defining means including means for injecting fuel 6 into said zone and means for defining passageways for selectively injecting gases selected from the group consisting of carbon dioxide containing gaseous combustion products and air and mixtures thereof into said zone concurrently with said fuel, c. at least a first one of said gas passageway defining means being for flowing gas including carbon dioxide concurrently with said fuel to effect an ignited a. means defining a combustion zone having an exit for gaseous combustion products formed therein,
  • burner means in communication with said combustion zone in its upstream region, said burner means including nozzle means for injecting finely divided fuel in a downstream direction into said combustion zone,
  • c. means having an aperture transverse to the path of fuel emitted from said nozzle
  • a source of carbon dioxide containing exhaust means being aligned with said aperture for projecting said fuel substantially centrally thereof.
  • Wlll react to form substantial amounts of carbon be monoxide
  • the quantity of exhaust gas introduced with said nozzle means fd r ffifi ectingfti el in c l ow nsl re aiir l fuel is about 10 to pefcem of the tolal flow direction into said Combustion Zone 30 of exhaust gases resultmg from burning said fuel c.
  • first means constructed and arranged for directing iss; 2 2;? g gg l fg i g 29 includedin combustion supporting gases in a generally down- 'flowin the ase S co b n d stream direction and in surrounding relationship in Ou m us lo pro uc S pm respect to Said nozzle means, prised n said combustion zone through means for d.
  • second means for conducting to said first means 35 prodlicmg a pletssure drop to thereby Increase the less than the amount of oxygen containing air revelocity of Sald p.mducts. turbulence quired for stoichiometric combustion of said fuel thereof for promoting fhelr mlxmg hence such that the combustion products in an upstream more complete region of said combustion zone resulting from reac-
  • a method ofbummg fuel .compnsed .Subsmmlany tion of said air with Said fuel will comprise 40 of hydrocarbons to reduce nitrogen oxides, carbon pletely and incompletely Oxidized combustion monoxide, unburned hydrocarbons and carbonaceous products including particulate carbon particulates m the exhaust gases therefrom, comprise.
  • said first means comprises a chamber for receiving P d s to a Substantial extent te Said Products said less than the stoichiometric amount of air and a ost me t, Said dditional gas ncluding id carbon di id t i i g gas, at least a substantial part ofthe remainder of the b.
  • means in said chamber having an aperture for said oxygen required for complete oxidation of said fuel directing of said gaseous mixture, said nozzle to thereby oxidize said carbon monoxide to carbon dioxide.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
US432623A 1974-01-11 1974-01-11 Pollutant reduction with selective gas stack recirculation Expired - Lifetime US3868211A (en)

Priority Applications (13)

Application Number Priority Date Filing Date Title
US432623A US3868211A (en) 1974-01-11 1974-01-11 Pollutant reduction with selective gas stack recirculation
GB5093174A GB1464169A (en) 1974-01-11 1974-11-25 Pollutatnt reduction with selective gas stack recirculation
CA214,788A CA1042339A (en) 1974-01-11 1974-11-26 Pollutant reduction with selective gas stack recirculation
NL7415901A NL7415901A (nl) 1974-01-11 1974-12-06 Werkwijze voor het verbranden van een brandstof arvoor geschikte inrichting.
ZA00747776A ZA747776B (en) 1974-01-11 1974-12-06 Pollutant reduction with selective gas stack recirculation
FR7441278A FR2257861B1 (enrdf_load_stackoverflow) 1974-01-11 1974-12-13
BE151467A BE823312A (fr) 1974-01-11 1974-12-13 Procede et appareil de reduction de la teneur en polluants des gaz d'echappement de bruleurs alimentes en combustible hydrocarbone
DE2461078A DE2461078C2 (de) 1974-01-11 1974-12-23 Verfahren zur Verringerung des Gehalts an Stickstoffoxiden, Kohlenmonoxid und Kohlenstoff in einem Abgas, sowie Feuerungsanlage zur Durchführung des Verfahrens
CH1729274A CH592846A5 (enrdf_load_stackoverflow) 1974-01-11 1974-12-24
JP50003022A JPS50102933A (enrdf_load_stackoverflow) 1974-01-11 1974-12-24
IT31028/74A IT1028056B (it) 1974-01-11 1974-12-24 Procedimento ed apparecchiatura per la riduzione degli inqquinanti atmosferici mediante ricircolazione selettiva dei gas di ciminiera
ES433324A ES433324A1 (es) 1974-01-11 1974-12-24 Un metodo para quemar combustible y aparato para su reali- zacion.
JP1982058584U JPS58111U (ja) 1974-01-11 1982-04-23 燃料の燃焼装置

Applications Claiming Priority (1)

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US432623A US3868211A (en) 1974-01-11 1974-01-11 Pollutant reduction with selective gas stack recirculation

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US (1) US3868211A (enrdf_load_stackoverflow)
JP (2) JPS50102933A (enrdf_load_stackoverflow)
BE (1) BE823312A (enrdf_load_stackoverflow)
CA (1) CA1042339A (enrdf_load_stackoverflow)
CH (1) CH592846A5 (enrdf_load_stackoverflow)
DE (1) DE2461078C2 (enrdf_load_stackoverflow)
ES (1) ES433324A1 (enrdf_load_stackoverflow)
FR (1) FR2257861B1 (enrdf_load_stackoverflow)
GB (1) GB1464169A (enrdf_load_stackoverflow)
IT (1) IT1028056B (enrdf_load_stackoverflow)
NL (1) NL7415901A (enrdf_load_stackoverflow)
ZA (1) ZA747776B (enrdf_load_stackoverflow)

Cited By (52)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3910749A (en) * 1974-10-11 1975-10-07 James T Voorheis Induction burner
US3914090A (en) * 1971-05-13 1975-10-21 Engelhard Min & Chem Method and furnace apparatus
US4023921A (en) * 1975-11-24 1977-05-17 Electric Power Research Institute Oil burner for NOx emission control
US4089629A (en) * 1975-02-12 1978-05-16 Pietro Fascione Process and apparatus for controlled recycling of combustion gases
US4144017A (en) * 1976-11-15 1979-03-13 The Babcock & Wilcox Company Pulverized coal combustor
US4162890A (en) * 1977-05-02 1979-07-31 Bloom Engineering Company, Inc. Combustion apparatus
EP0007697A1 (en) * 1978-06-19 1980-02-06 John Zink Company Burner system for gaseous and/or liquid fuels with a minimum production of NOx
US4295822A (en) * 1979-10-01 1981-10-20 Campbell Crom B Producer gas fueled burner system and drying apparatus
US4421474A (en) * 1982-08-25 1983-12-20 Meyer Stanley A Hydrogen gas burner
US4422391A (en) * 1981-03-12 1983-12-27 Kawasaki Jukogyo Kabushiki Kaisha Method of combustion of pulverized coal by pulverized coal burner
US4547147A (en) * 1983-06-30 1985-10-15 Mitsubishi Denki Kabushiki Kaisha Combustion device for a car
WO1986001876A1 (en) * 1984-09-12 1986-03-27 Air (Anti Pollution Industrial Research) Ltd. Method and apparatus for conducting a substantially isothermal combustion process in a combustor
US4659305A (en) * 1985-12-30 1987-04-21 Aqua-Chem, Inc. Flue gas recirculation system for fire tube boilers and burner therefor
WO1988005762A1 (en) * 1987-02-02 1988-08-11 Fuel Tech, Inc. Process and apparatus for reducing the concentration of pollutants in an effluent
EP0227637A3 (en) * 1985-12-23 1988-09-21 Dr. Brucker & Zeman & Mag. Seyr Controlled Soft Combustion Gesellschaft Burgerlichen Rechts Oil burner
EP0279913A3 (en) * 1987-02-26 1989-05-03 Ingenieurbureau Sonvico Ag Burner for the combustion of liquid gaseous fuels
US4862835A (en) * 1987-11-04 1989-09-05 Deutsche Babcock Werke Aktiengesellschaft Combustion system for burning heavy heating oil with low nox
DE3832494A1 (de) * 1988-09-22 1990-03-29 Vaillant Joh Gmbh & Co Verfahren und vorrichtung zur speisung eines gasbrenners mit einem gemisch
US4926765A (en) * 1986-12-11 1990-05-22 Walter Dreizler Furnace blower with external gas recycling for the reduction of NOx
EP0391858A1 (de) * 1989-04-07 1990-10-10 BALSIGER, Benno Vorrichtung zur Rauchgasrückführung bei Oel- und Gasbrennern
US4995807A (en) * 1989-03-20 1991-02-26 Bryan Steam Corporation Flue gas recirculation system
US5127821A (en) * 1989-04-24 1992-07-07 Asea Brown Boveri Ltd. Premixing burner for producing hot gas
US5129818A (en) * 1990-09-14 1992-07-14 Benno Balsiger Method of feeding back exhaust gases in oil and gas burners
US5193995A (en) * 1987-12-21 1993-03-16 Asea Brown Boveri Ltd. Apparatus for premixing-type combustion of liquid fuel
US5195883A (en) * 1992-04-01 1993-03-23 Aqua-Chem, Inc. Flue gas recirculation system with fresh air purge for burners
US5241915A (en) * 1992-08-10 1993-09-07 Consolidated Natural Gas Service Company, Inc. Apparatus and method to improve pulverizer and reduce NOx emissions in coal-fired boilers
US5269679A (en) * 1992-10-16 1993-12-14 Gas Research Institute Staged air, recirculating flue gas low NOx burner
FR2711224A1 (fr) * 1993-10-12 1995-04-21 Guillot Ind Sa Dispositif de chauffage à recyclage partiel des gaz de combustion.
US5413477A (en) * 1992-10-16 1995-05-09 Gas Research Institute Staged air, low NOX burner with internal recuperative flue gas recirculation
US5427525A (en) * 1993-07-01 1995-06-27 Southern California Gas Company Lox NOx staged atmospheric burner
US5453004A (en) * 1993-03-23 1995-09-26 Viessmann Werke Gmbh & Co. Method for operation of an oil evaporation burner and an oil evaporation burner for carrying out the method
US5527984A (en) * 1993-04-29 1996-06-18 The Dow Chemical Company Waste gas incineration
US5560710A (en) * 1988-12-23 1996-10-01 Thyssengas Gmbh Process for mixing gas jets or streams
US5769010A (en) * 1996-02-01 1998-06-23 Btu International, Inc. Furnace including localized incineration of effluents
US6039560A (en) * 1996-01-31 2000-03-21 Sanyo Electric Co., Ltd. Low NOx burner and method of controlling recirculation of exhaust gas
EP1016822A1 (en) * 1998-12-30 2000-07-05 IPEG S.p.A. dell'Ing. Mauro Poppi Combustion air feeder for high heat release burner of kilns
US6200128B1 (en) * 1997-06-09 2001-03-13 Praxair Technology, Inc. Method and apparatus for recovering sensible heat from a hot exhaust gas
EP1094275A1 (en) * 1999-10-21 2001-04-25 IPEG S.p.A. dell'Ing. Mauro Poppi Valve for recirculating combustion gas ducts
US6302683B1 (en) * 1996-07-08 2001-10-16 Ab Volvo Catalytic combustion chamber and method for igniting and controlling the catalytic combustion chamber
DE4131975C2 (de) * 1990-10-01 2002-09-12 Remac Umwelttechnik R Mark Anordnung zur Reduktion von Stickstoffoxyden im Abgas einer Feuerungsanlage
US20040146820A1 (en) * 2003-01-14 2004-07-29 Richard Carroni Combustion method and burner for carrying out the method
US20040228786A1 (en) * 2003-02-03 2004-11-18 Walter Schicketanz Oxidative purification of a flue gas containing oxygen and a combustible component
US20050150211A1 (en) * 2004-01-13 2005-07-14 Crawley Wilbur H. Method and apparatus for directing exhaust gas through a fuel-fired burner of an emission abatement assembly
US20080182214A1 (en) * 2006-10-19 2008-07-31 Wayne/Scott Fetzer Company Modulated power burner system and method
CN101806449A (zh) * 2010-03-04 2010-08-18 郑宗标 一种燃气锅炉
WO2011012452A1 (de) * 2009-07-31 2011-02-03 Siemens Vai Metals Technologies Gmbh Reformergasbasiertes reduktionsverfahren mit vermindertem nox-ausstoss
US20120012036A1 (en) * 2010-07-15 2012-01-19 Shaw John R Once Through Steam Generator
US20120214116A1 (en) * 2011-02-22 2012-08-23 Cameron Andrew M Apparatus and method for heating a blast furnace stove
WO2012065691A3 (de) * 2010-11-18 2013-08-08 Linde Aktiengesellschaft Brenner mit einstellbarer rauchgasrezirkulation
US20180149355A1 (en) * 2016-11-28 2018-05-31 Neeraj Saxena Heat treatment process with oxygen enhancement of air-fuel burners
CN114353058A (zh) * 2021-12-06 2022-04-15 浙江京洋环保科技有限公司 一种降低燃煤锅炉二氧化碳排放浓度的燃烧方法
US11933491B2 (en) 2016-06-07 2024-03-19 The Cleaver-Brooks Company, LLC Burner with adjustable end cap and method of operating same

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SE442053B (sv) * 1984-04-17 1985-11-25 Nils Axel Ambjoern Oestbo Turbulator
DE3713408A1 (de) * 1987-04-21 1988-11-03 Weishaupt Max Gmbh Verfahren zur reduzierung von no(pfeil abwaerts)x(pfeil abwaerts)-werten bei oel- oder gasbetriebenen feuerungsanlagen
DE3937925C2 (de) * 1989-11-15 1994-06-09 Electro Oil Gmbh Brennerkopf für einen Ölbrenner
DE9004612U1 (de) * 1990-04-24 1991-08-22 Vießmann, Hans, Dr.h.c., 3559 Battenberg Öl- oder Gasgebläsebrenner
DE4301840C2 (de) * 1993-01-23 1995-06-14 Riedhammer Gmbh Co Kg Gasbrenner für Öfen und Feuerungsanlagen
DE19606733C1 (de) 1996-02-23 1997-05-07 Viessmann Werke Kg Verfahren zum Betrieb insbesondere eines Ölvergasungsbrenners und Brenner zu seiner Durchführung
WO1999061839A1 (en) * 1998-05-25 1999-12-02 Wedab Wave Energy Development Ab A boiler arrangement and a method of burning oil

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3146821A (en) * 1960-08-29 1964-09-01 Fred H Wuetig Method of and apparatus for governing the operation of furnaces
US3730668A (en) * 1971-03-03 1973-05-01 Tokyo Gas Co Ltd Combustion method of gas burners for suppressing the formation of nitrogen oxides and burner apparatus for practicing said method
US3746498A (en) * 1972-01-24 1973-07-17 Combustion Eng Reducing no{11 {11 emissions by additive injection
US3781162A (en) * 1972-03-24 1973-12-25 Babcock & Wilcox Co Reducing nox formation by combustion

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS4829023A (enrdf_load_stackoverflow) * 1971-01-22 1973-04-17
NL7200207A (enrdf_load_stackoverflow) * 1972-01-06 1973-07-10
JPS4950710A (enrdf_load_stackoverflow) * 1972-09-18 1974-05-17
JPS6039826B2 (ja) * 1977-06-09 1985-09-07 石川 尭 建築用発泡石こうパネル及び製造法

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3146821A (en) * 1960-08-29 1964-09-01 Fred H Wuetig Method of and apparatus for governing the operation of furnaces
US3730668A (en) * 1971-03-03 1973-05-01 Tokyo Gas Co Ltd Combustion method of gas burners for suppressing the formation of nitrogen oxides and burner apparatus for practicing said method
US3746498A (en) * 1972-01-24 1973-07-17 Combustion Eng Reducing no{11 {11 emissions by additive injection
US3781162A (en) * 1972-03-24 1973-12-25 Babcock & Wilcox Co Reducing nox formation by combustion

Cited By (63)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3914090A (en) * 1971-05-13 1975-10-21 Engelhard Min & Chem Method and furnace apparatus
US3910749A (en) * 1974-10-11 1975-10-07 James T Voorheis Induction burner
US4089629A (en) * 1975-02-12 1978-05-16 Pietro Fascione Process and apparatus for controlled recycling of combustion gases
US4023921A (en) * 1975-11-24 1977-05-17 Electric Power Research Institute Oil burner for NOx emission control
US4144017A (en) * 1976-11-15 1979-03-13 The Babcock & Wilcox Company Pulverized coal combustor
US4162890A (en) * 1977-05-02 1979-07-31 Bloom Engineering Company, Inc. Combustion apparatus
EP0007697A1 (en) * 1978-06-19 1980-02-06 John Zink Company Burner system for gaseous and/or liquid fuels with a minimum production of NOx
US4295822A (en) * 1979-10-01 1981-10-20 Campbell Crom B Producer gas fueled burner system and drying apparatus
US4422391A (en) * 1981-03-12 1983-12-27 Kawasaki Jukogyo Kabushiki Kaisha Method of combustion of pulverized coal by pulverized coal burner
US4421474A (en) * 1982-08-25 1983-12-20 Meyer Stanley A Hydrogen gas burner
US4547147A (en) * 1983-06-30 1985-10-15 Mitsubishi Denki Kabushiki Kaisha Combustion device for a car
WO1986001876A1 (en) * 1984-09-12 1986-03-27 Air (Anti Pollution Industrial Research) Ltd. Method and apparatus for conducting a substantially isothermal combustion process in a combustor
EP0227637A3 (en) * 1985-12-23 1988-09-21 Dr. Brucker & Zeman & Mag. Seyr Controlled Soft Combustion Gesellschaft Burgerlichen Rechts Oil burner
US4659305A (en) * 1985-12-30 1987-04-21 Aqua-Chem, Inc. Flue gas recirculation system for fire tube boilers and burner therefor
US4926765A (en) * 1986-12-11 1990-05-22 Walter Dreizler Furnace blower with external gas recycling for the reduction of NOx
US4842834A (en) * 1987-02-02 1989-06-27 Fuel Tech, Inc. Process for reducing the concentration of pollutants in an effluent
WO1988005762A1 (en) * 1987-02-02 1988-08-11 Fuel Tech, Inc. Process and apparatus for reducing the concentration of pollutants in an effluent
EP0279913A3 (en) * 1987-02-26 1989-05-03 Ingenieurbureau Sonvico Ag Burner for the combustion of liquid gaseous fuels
US4862835A (en) * 1987-11-04 1989-09-05 Deutsche Babcock Werke Aktiengesellschaft Combustion system for burning heavy heating oil with low nox
US5193995A (en) * 1987-12-21 1993-03-16 Asea Brown Boveri Ltd. Apparatus for premixing-type combustion of liquid fuel
DE3832494A1 (de) * 1988-09-22 1990-03-29 Vaillant Joh Gmbh & Co Verfahren und vorrichtung zur speisung eines gasbrenners mit einem gemisch
US5560710A (en) * 1988-12-23 1996-10-01 Thyssengas Gmbh Process for mixing gas jets or streams
US4995807A (en) * 1989-03-20 1991-02-26 Bryan Steam Corporation Flue gas recirculation system
EP0391858A1 (de) * 1989-04-07 1990-10-10 BALSIGER, Benno Vorrichtung zur Rauchgasrückführung bei Oel- und Gasbrennern
US5127821A (en) * 1989-04-24 1992-07-07 Asea Brown Boveri Ltd. Premixing burner for producing hot gas
US5129818A (en) * 1990-09-14 1992-07-14 Benno Balsiger Method of feeding back exhaust gases in oil and gas burners
DE4131975C2 (de) * 1990-10-01 2002-09-12 Remac Umwelttechnik R Mark Anordnung zur Reduktion von Stickstoffoxyden im Abgas einer Feuerungsanlage
US5195883A (en) * 1992-04-01 1993-03-23 Aqua-Chem, Inc. Flue gas recirculation system with fresh air purge for burners
US5241915A (en) * 1992-08-10 1993-09-07 Consolidated Natural Gas Service Company, Inc. Apparatus and method to improve pulverizer and reduce NOx emissions in coal-fired boilers
US5269679A (en) * 1992-10-16 1993-12-14 Gas Research Institute Staged air, recirculating flue gas low NOx burner
US5413477A (en) * 1992-10-16 1995-05-09 Gas Research Institute Staged air, low NOX burner with internal recuperative flue gas recirculation
US5453004A (en) * 1993-03-23 1995-09-26 Viessmann Werke Gmbh & Co. Method for operation of an oil evaporation burner and an oil evaporation burner for carrying out the method
US5527984A (en) * 1993-04-29 1996-06-18 The Dow Chemical Company Waste gas incineration
US5427525A (en) * 1993-07-01 1995-06-27 Southern California Gas Company Lox NOx staged atmospheric burner
FR2711224A1 (fr) * 1993-10-12 1995-04-21 Guillot Ind Sa Dispositif de chauffage à recyclage partiel des gaz de combustion.
US6039560A (en) * 1996-01-31 2000-03-21 Sanyo Electric Co., Ltd. Low NOx burner and method of controlling recirculation of exhaust gas
US5769010A (en) * 1996-02-01 1998-06-23 Btu International, Inc. Furnace including localized incineration of effluents
US6302683B1 (en) * 1996-07-08 2001-10-16 Ab Volvo Catalytic combustion chamber and method for igniting and controlling the catalytic combustion chamber
US6200128B1 (en) * 1997-06-09 2001-03-13 Praxair Technology, Inc. Method and apparatus for recovering sensible heat from a hot exhaust gas
EP1016822A1 (en) * 1998-12-30 2000-07-05 IPEG S.p.A. dell'Ing. Mauro Poppi Combustion air feeder for high heat release burner of kilns
EP1094275A1 (en) * 1999-10-21 2001-04-25 IPEG S.p.A. dell'Ing. Mauro Poppi Valve for recirculating combustion gas ducts
US6896509B2 (en) * 2003-01-14 2005-05-24 Alstom Technology Ltd Combustion method and burner for carrying out the method
US20040146820A1 (en) * 2003-01-14 2004-07-29 Richard Carroni Combustion method and burner for carrying out the method
US20040228786A1 (en) * 2003-02-03 2004-11-18 Walter Schicketanz Oxidative purification of a flue gas containing oxygen and a combustible component
US20050150211A1 (en) * 2004-01-13 2005-07-14 Crawley Wilbur H. Method and apparatus for directing exhaust gas through a fuel-fired burner of an emission abatement assembly
US8641411B2 (en) * 2004-01-13 2014-02-04 Faureua Emissions Control Technologies, USA, LLC Method and apparatus for directing exhaust gas through a fuel-fired burner of an emission abatement assembly
US20080182214A1 (en) * 2006-10-19 2008-07-31 Wayne/Scott Fetzer Company Modulated power burner system and method
US20100319551A1 (en) * 2006-10-19 2010-12-23 Wayne/Scott Fetzer Company Modulated Power Burner System And Method
US8075304B2 (en) 2006-10-19 2011-12-13 Wayne/Scott Fetzer Company Modulated power burner system and method
US9719683B2 (en) 2006-10-19 2017-08-01 Wayne/Scott Fetzer Company Modulated power burner system and method
WO2011012452A1 (de) * 2009-07-31 2011-02-03 Siemens Vai Metals Technologies Gmbh Reformergasbasiertes reduktionsverfahren mit vermindertem nox-ausstoss
US10030911B2 (en) 2009-07-31 2018-07-24 Primetals Technologies Austria GmbH Reformer gas-based reducing method with reduced NOx emission
CN102471811A (zh) * 2009-07-31 2012-05-23 西门子Vai金属科技有限责任公司 基于转化炉气的具有降低的NOx排放的还原方法
US9181595B2 (en) 2009-07-31 2015-11-10 Siemens Vai Metals Technologies Gmbh Reformer gas-based reducing method with reduced NOx emission
CN101806449A (zh) * 2010-03-04 2010-08-18 郑宗标 一种燃气锅炉
CN101806449B (zh) * 2010-03-04 2011-11-23 郑宗标 一种燃气锅炉
US20120012036A1 (en) * 2010-07-15 2012-01-19 Shaw John R Once Through Steam Generator
WO2012065691A3 (de) * 2010-11-18 2013-08-08 Linde Aktiengesellschaft Brenner mit einstellbarer rauchgasrezirkulation
US20120214116A1 (en) * 2011-02-22 2012-08-23 Cameron Andrew M Apparatus and method for heating a blast furnace stove
US9863013B2 (en) * 2011-02-22 2018-01-09 Linde Aktiengesellschaft Apparatus and method for heating a blast furnace stove
US11933491B2 (en) 2016-06-07 2024-03-19 The Cleaver-Brooks Company, LLC Burner with adjustable end cap and method of operating same
US20180149355A1 (en) * 2016-11-28 2018-05-31 Neeraj Saxena Heat treatment process with oxygen enhancement of air-fuel burners
CN114353058A (zh) * 2021-12-06 2022-04-15 浙江京洋环保科技有限公司 一种降低燃煤锅炉二氧化碳排放浓度的燃烧方法

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JPS50102933A (enrdf_load_stackoverflow) 1975-08-14
JPS58111U (ja) 1983-01-05
DE2461078A1 (de) 1975-07-17
DE2461078C2 (de) 1983-05-05
BE823312A (fr) 1975-04-01
GB1464169A (en) 1977-02-09
NL7415901A (nl) 1975-07-15
ZA747776B (en) 1976-01-28
CH592846A5 (enrdf_load_stackoverflow) 1977-11-15
FR2257861A1 (enrdf_load_stackoverflow) 1975-08-08
CA1042339A (en) 1978-11-14
FR2257861B1 (enrdf_load_stackoverflow) 1978-10-13
IT1028056B (it) 1979-01-30
ES433324A1 (es) 1976-11-16

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