EP0451648A2 - Drehrohrofen mit gegeneinander gerichteten Flammen - Google Patents

Drehrohrofen mit gegeneinander gerichteten Flammen Download PDF

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Publication number
EP0451648A2
EP0451648A2 EP91105063A EP91105063A EP0451648A2 EP 0451648 A2 EP0451648 A2 EP 0451648A2 EP 91105063 A EP91105063 A EP 91105063A EP 91105063 A EP91105063 A EP 91105063A EP 0451648 A2 EP0451648 A2 EP 0451648A2
Authority
EP
European Patent Office
Prior art keywords
oxidant
cylindrical body
rotatable cylindrical
flue
injected
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP91105063A
Other languages
English (en)
French (fr)
Other versions
EP0451648A3 (en
EP0451648B1 (de
Inventor
Min-Da Ho
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Praxair Technology Inc
Original Assignee
Union Carbide Industrial Gases Technology Corp
Praxair Technology Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Union Carbide Industrial Gases Technology Corp, Praxair Technology Inc filed Critical Union Carbide Industrial Gases Technology Corp
Publication of EP0451648A2 publication Critical patent/EP0451648A2/de
Publication of EP0451648A3 publication Critical patent/EP0451648A3/en
Application granted granted Critical
Publication of EP0451648B1 publication Critical patent/EP0451648B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/20—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having rotating or oscillating drums
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • 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
    • F23C9/006—Combustion apparatus characterised by arrangements for returning combustion products or flue gases to the combustion chamber the recirculation taking place in the combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/12—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating using gaseous or liquid fuel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
    • F27B7/34—Arrangements of heating devices
    • 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
    • F23C2202/40—Inducing local whirls around flame

Definitions

  • This invention relates generally to rotary kilns and is particularly useful with mobile rotary kilns.
  • a rotary kiln is a refractory-lined cylindrical vessel commonly used, for example, in the incineration of waste, in the calcining of cement, coke or other materials, in the firing of ceramic, and in many other uses.
  • the waste is provided into the kiln and is combusted while passing through the kiln by the combustion fuel and oxidant which is injected into the rotary kiln at one end of the kiln.
  • the injection of the fuel and oxidant into the kiln may be either concurrent with the flow of waste or other material through the kiln, or it may be countercurrent to the flow of waste or other material through the kiln.
  • Gases from within the kiln are removed through a flue located at one end of the kiln. After the waste has passed through the kiln, ash from the combusted waste is removed from the kiln.
  • the throughput of material, such as waste, through the kiln is limited by the quantity of furnace gases generated within the kiln by the injected fuel and oxidant, and by the combusting volatiles if volatiles are present, and also by the rate at which heat can be transferred to wet material or to other heat sinks by the furnace gases.
  • a recent use for rotary kilns which has been gaining wide acceptance has been in the incineration of hazardous waste.
  • a particularly advantageous rotary kiln for this application is a mobile or transportable rotary kiln which can be transported to the hazardous waste site and then removed when the hazardous waste site has been cleaned.
  • a mobile rotary kiln is by necessity smaller than a stationary rotary kiln in order to enable transportability.
  • the throughput limitations discussed above are even more acute in the case of a mobile rotary kiln.
  • a rotary kiln comprising:
  • Another aspect of this invention comprises: A method for operating a rotary kiln comprising:
  • cylindrical means tubular, generally but not necessarily having a circular radial cross-section.
  • waste means any material intended for partial or total combustion within a combustion zone.
  • burner means a device through which both oxidant and combustible matter are provided into a combustion zone either separately or as a mixture.
  • the term "lance” means a device through which either oxidant or combustible matter but not both is provided into a combustion zone.
  • recirculation ratio means the ratio of the mass flowrate of material recirculated back toward the periphery of a jet to the mass flowrate of the total fluid injected into a combustion zone.
  • combustion means a substance that will burn under combustion zone conditions.
  • incombustible means a substance that will not burn under combustion zone conditions.
  • volatile means a material which will pass into the vapor state under combustion zone conditions such as, for example, the vapor materials resulting from drying, or from the decomposition or thermal dissociation of solid or liquid materials.
  • equivalent diameter means that diameter of a single circular orifice which would provide the same total area as the sum of the areas of a multi-orifice injection means.
  • Figure 1 is a schematic representation of one embodiment of the invention carried out in conjunction with waste incineration within a countercurrent kiln.
  • Figure 2 is a schematic representation of another embodiment of the invention carried out in conjunction with waste incineration within a concurrent kiln.
  • Figure 3 is a schematic representation of another embodiment of the invention illustrating the invention carried out with a plug flow zone.
  • Figure 4 is an illustration of a single orifice oxidant injection means for injecting oxidant with a high momentum into a kiln at the flue end.
  • Figure 5 is an illustration of a multi-orifice oxidant injection means for injecting oxidant with a high momentum into a kiln at the flue end.
  • FIG. 6 is an illustration of a burner which may be used in the practice of this invention.
  • Figure 7 is an illustration of a means to react fuel and oxidant in a recessed cavity prior to injection into the kiln.
  • the invention enables a significant increase in rotary kiln throughput by maintaining a desirable temperature profile throughout the kiln. This reduces large temperature gradients through the kiln reducing the need for a high temperature in one part of the kiln in order to provide heat to another part of the kiln. In addition the need for auxiliary fuel combustion to provide heat to a drying zone within the kiln is reduced. Thus throughput limitations caused by localized hot temperatures or flue gas flowrates are relaxed.
  • rotary kiln 1 having a rotatable cylindrical body 2, and nonrotatable walls 3 and 4 at each axial end of the rotatable cylindrical body to define a combustion zone 5.
  • the kiln has a length to diameter ratio exceeding 4 but less than 8.
  • Flue 6 is positioned at one axial end of rotatable cylindrical body 2. Although shown in Figure 1 as having a horizontal orientation, the flue may have a vertical or any other suitable orientation.
  • a first oxidant injection means such as first burner 7 is positioned within nonrotatable wall 4 opposite the end having flue 6. First burner 7 is oriented to inject fuel and oxidant into combustion zone 5 within rotatable cylindrical body 2 in a direction toward the flue end.
  • Second oxidant injection means such as second burner 8 is positioned within nonrotatable wall 3 at the flue end and is oriented to inject fuel and oxidant into combustion zone 5 in a direction toward the end opposite the flue end.
  • either or both of the first and second oxidant injection means may be a lance, such as lance 12. In such a case only oxidant is provided into the combustion zone from a lance.
  • the second oxidant injection means which injects oxidant into the kiln in the direction away from the flue end is adapted to inject the oxidant with a momentum sufficient to pass through the kiln a length equal to at least two times the internal diameter of, and preferably at least 50 percent of the length of, the rotatable cylindrical body.
  • One means of accomplishing this high momentum is by the injection of the oxidant through a restricted orifice having a diameter, or multiple orifices having an equivalent diameter, not exceeding 1/30 of the kiln internal diameter and preferably not exceeding 1/100 of the kiln internal diameter.
  • the restricted orifice imparts a high velocity to the oxidant as defined by Bernoulli's equation, and the high velocity causes the momentum to increase since momentum is the product of mass and velocity.
  • Another means of accomplishing high momentum is by increasing the mass of the second oxidant. However, this is not preferable because this simultaneously increases the mass and the momentum of the gas flowing toward the flue end.
  • Figures 4, 5 and 6 illustrate such second oxidant injection means.
  • a single orifice nozzle having a restricted diameter for the injection of oxidant there is illustrated a single orifice nozzle having a restricted diameter for the injection of oxidant.
  • Figure 5 illustrates a multiple orifice nozzle having an equivalent diameter of the defined restriction to enable the attainment of the required high momentum.
  • Figure 6 illustrates a burner wherein oxidant and fuel may be injected through concentric tubes to produce oxidizing gas. Oxidant may be fed through the center tube and fuel may be fed through the outer annular passage or vice versa.
  • the center tube may be fitted with a single or a multiple orifice nozzle.
  • oxidant and some fuel can react and expand within a cavity recessed within the kiln wall.
  • the cavity provides a restriction so that the hot combustion products at near the adiabatic flame temperature of the mixture leave the cavity at a high velocity.
  • the cavity would have a diameter at the point of communication with the kiln of less than 1/10 of the kiln internal diameter.
  • feed such as waste 9, comprising volatile material is provided into combustion zone 5, such as through ram feeder 10, to form a bed which flows through the combustion zone.
  • Other feeds which be used with this invention include cement, coke, ceramic and other materials which include a volatile component such as water.
  • the method of this invention will be described in detail with waste as the feed which may include volatile combustible and volatile incombustible matter.
  • Waste may be liquid and/or solid waste such as is defined in the Resource Conservation Recovery Act (RCRA) or the Toxic Substances Control Act (TSCA).
  • the waste passes sequentially through a drying zone 13 wherein it is dried of volatile incombustible matter such as water and some of the lighter volatile combustible matter, a pyrolysis zone 14 wherein additional combustible matter is volatized out, and a char burnout zone 15 wherein the residual solids are combusted.
  • Resulting ash is removed from combustion zone 5 through ash removal door 11.
  • ash removal door 11 As is appreciated by one skilled in the art, there is not a clear demarcation between these zones.
  • the arrows indicate the volatization of incombustible and combustible matter in zones 13 and 14 respectively.
  • Fuel and oxidant are injected through burner 7 into combustion zone 5 wherein they are combusted to provide heat to the combustion zone to carry out the drying, pyrolyzing and burning of the waste discussed above.
  • the oxidant may be air, technically pure oxygen having an oxygen concentration greater than 99.5 percent, or oxygen-enriched air having an oxygen concentration of at least 25 percent and preferably greater than 30 percent.
  • the fuel may be any suitable fluid fuel such as natural gas, propane, fuel oil, or liquid waste.
  • Fuel and oxidant are injected into combustion zone 5 through second burner 8 and can be defined the same as the fuel and oxidant injected through first burner 7.
  • the fuel and oxidant injected through burner 8 is injected having a momentum at least equal to, and preferably greater than 200 percent of, the momentum of the gas flowing toward the flue end.
  • the gas flowing toward the flue end may include fuel and oxidant injected through the first burner and the combustion products thereof, water vapor, combustion products from the material injected through the second burner, and combustion products from the combustion of volatized combustible material.
  • momentum is equal to the mass times the velocity of the fluid.
  • the combustion reaction stream injected through burner 8 penetrates a significant distance into combustion zone 5, preferably at least two kiln diameters. Heat released from the combustion of the fuel and oxidant injected into combustion zone 5 through burner 8 serves to provide heat for the aforedescribed drying, pyrolyzing and burning of the waste.
  • the arrangement of the invention wherein burners fire opposed to one another causes the temperature within the combustion zone to be much more uniform than with conventional rotary kiln arrangements because the two injected combustion streams tend to cause each other to recirculate through the combustion zone as indicated by the reversing flow arrows 16 in Figure 1, although only the recirculation of the gas flowing from the flue end is necessary for the successful operation of the invention.
  • the high momentum of the flue end combustion stream causes enhanced recirculation as shown by arrows 17. In this way temperature gradients within the kiln are better controlled so throughput limitations based on heat transfer rate considerations or flue gas flowrate considerations are relaxed.
  • the high momentum flame may be manipulated to enhance local radiative and convective heat transfer to the load when desired.
  • either or both of the oxidant streams injected through oxidant injection means 7 and 8 are injected at a high velocity so as to provide a recirculation of gases within the combustion zone, preferably to provide a recirculation ratio exceeding 4.
  • the oxidant stream velocity exceeds 150 feet per second. In this way the temperature uniformity within combustion zone 5 is enhanced. This is particularly the case for the oxidant stream injected through first burner 7 so that, as illustrated in Figure 1, the gases do not merely pass through combustion zone 5, but rather recirculate one or more times within combustion zone 5 so as to enhance mixing and combustion efficiency within combustion zone 5 and thus further enhance temperature uniformity within each of the two recirculation zones at the two parts of the combustion zone.
  • the injection end of the second oxidant injection means located at the flue end protrudes a distance into the combustion zone as illustrated in Figure 3 rather than having its injection end flush with the wall within which it is positioned as is illustrated in Figures 1 and 2.
  • the numerals in Figure 3 correspond to those of Figure 1 for the common elements.
  • a plug flow zone is establish immediately before the flue.
  • the gas velocity is reduced due to the lack of recirculation flow. Therefore, air-borne particulates have the opportunity to settle down from the gas stream. Also the gas is allowed to cool down somewhat, resulting in reduced gas velocity.
  • the protrusion can be as long as practical and typically is about one kiln diameter.
  • a countercurrent kiln it may be desirable to inject additional oxidant, such as technically pure oxygen, into the combustion zone at the flue end in order to carry out further combustion in the drying zone.
  • additional oxidant such as technically pure oxygen
  • the additional oxidant may be injected through burner 8 or through lance 12 depending on which is used as the second oxidant injection means.
  • the invention enables the kiln operator to operate the combustion zone of the rotary kiln with two separate combustion control zones at each end of the kiln.
  • the combustion control zone at each end of the kiln may be operated with pyrolytic (fuel-rich) or oxidating (oxygen-rich) conditions thus adding flexibility to the kiln design and to the combustion process control.
  • the combustion control zone at the flue end of a countercurrent rotary kiln can be run in the pyrolytic mode so that combustible gases released from the waste are recirculated and entrained into the high momentum stream from the flue end burner thus consuming the oxidant.
  • Residue char in the combustion control zone at the other end of the kiln can be exposed to oxidating conditions to complete the burnout.
  • the use of oxygen enrichment serves to decrease the momentum of the gases flowing toward the flue thus enabling easier flue end injection into the kiln, and also serves to decrease the volumetric flowrate of gases flowing through the flue thus increasing throughput. Accordingly the lower the percentage of inert nitrogen introduced into the combustion zone with the oxidant, the more advantageous will be the operation of the method of this invention. Thus, to achieve maximum throughput, the most preferred oxidant is technically pure oxygen, air inleakage notwithstanding.
  • Figure 2 illustrates the rotary kiln and operating method of this invention carried out with the incineration of waste in a concurrent kiln.
  • flue 20 is located at the end opposite the end at which waste is provided into the kiln.
  • First oxidant injection means such as a lance or burner 21 is positioned within nonrotatable wall 3 at the end opposite the flue end and second oxidant injection means such as a lance or burner 22 is positioned within nonrotatable wall 4 at the flue end.
  • Oxidant injection means 21 and 22 inject oxidant toward the wall opposite from where they are positioned.
  • the invention enables the operation of a rotary kiln with improved control by enabling independent or separate adjustment of the oxidant and fluid fuel injected at the flue end and at the end opposite the flue end. This is particularly advantageous when these two oxidants have differing oxygen concentrations, e.g. air and technically pure oxygen.
  • determine means any way of arriving at a value including measuring, calculating or estimating the value.
  • the flowrate may then be compared with a predetermined desired flowrate and the flowrate ratio of the oxidants may then be adjusted, i.e. changed, so that the determined flowrate changes in the direction toward the desired flowrate. Because of the high momentum of the oxidant injected at the flue end which passes significant gas flow away from the flue into the kiln, as opposed to prior art processes, changes in flue gas flowrate can be accomplished with changes in the flowrate ratio of the injected oxidants while being able to maintain a desirable temperature profile and furnace atmosphere.
  • any operating parameter may be determined, compared with a predetermined desired value for that parameter, and the total flowrate and the flowrate ratio of the oxidants may be adjusted so that the determined value of the parameter changes in the direction toward the desired value for that parameter.
  • this advantageous control based on changing the total flowrate and the ratio of the oxidants is due to the high momentum of the flue end injected oxidant which doesn't merely affect the proximity of the flue end as in conventional processes, but rather has a marked effect on the gas flow pattern within the kiln.
  • a significant advantage of the invention is the ability to independently control temperature or heat release and atmosphere at each end of the kiln while simultaneously controlling gas flowrate or pressure in the kiln.
  • Temperature within the kiln may also be controlled or moderated by the injection of water, especially as an atomized stream, into the kiln.
  • a scaled-down cold flow model of a rotary kiln similar to that illustrated in Figure 3 was employed.
  • the kiln model had a length of 3.5 feet and an L/D ratio of 7.
  • the momentum of the flow from the burner ranged between 100 to 500 percent of the momentum of the gases flowing toward the flue.
  • the flow from the flue end jet penetrated up to 63.3 percent of the length of the kiln. Recirculation gas flow within the kiln flue end was vigorous.
  • a countercurrent rotary kiln similar to that illustrated in Figure 3 is employed having a length of 45 feet and an internal diameter of 6.5 feet.
  • Oxygen at a flowrate of 4092 lb/hr and natural gas at a flowrate of 1066 lb/hr, having a heat value of 22,991 BTU/lb, are injected at a high momentum into the kiln at the flue end through a burner extending 5 feet into the kiln.
  • Air at a flowrate of 11,000 lb/hr and natural gas at a flowrate of 613 lb/hr are injected into the kiln through a burner at the end opposite the flue end.
  • the kiln is operated at negative pressure and ambient air leaks into the kiln at a flowrate of 5500 lb/hr.
  • Soil comprising hazardous waste and having a water content of 15 percent but no heating value is passed into the kiln at the flue end at the rate of 25 tons per hour.
  • Ash is removed from the kiln at a temperature of 900°F at a flowrate of 42,494 lb/hr and gas is passed out of the kiln through the flue at the rate of 29,777 lb/hr (30,630 actual cubic feed per minute) at a temperature of 1600°F and having an oxygen concentration of 3.1 percent.
  • the maximum soil processing rate is only 16 tons per hour while meeting the required ash temperature of 900°F.
  • the flame is shortened and the combustion gas temperature gradient is significantly increased so that, at an increased throughput, the soil does not undergo sufficient residence time at the elevated temperature to undergo a detoxification reaction.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Incineration Of Waste (AREA)
  • Muffle Furnaces And Rotary Kilns (AREA)
  • Thermotherapy And Cooling Therapy Devices (AREA)
  • Soy Sauces And Products Related Thereto (AREA)
  • Treatment Of Fiber Materials (AREA)
EP91105063A 1990-03-29 1991-03-28 Drehrohrofen mit gegeneinander gerichteten Flammen Expired - Lifetime EP0451648B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US50090690A 1990-03-29 1990-03-29
US500906 1990-03-29

Publications (3)

Publication Number Publication Date
EP0451648A2 true EP0451648A2 (de) 1991-10-16
EP0451648A3 EP0451648A3 (en) 1992-05-13
EP0451648B1 EP0451648B1 (de) 1993-05-05

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EP91105063A Expired - Lifetime EP0451648B1 (de) 1990-03-29 1991-03-28 Drehrohrofen mit gegeneinander gerichteten Flammen

Country Status (7)

Country Link
EP (1) EP0451648B1 (de)
JP (1) JPH04225783A (de)
KR (1) KR960010601B1 (de)
BR (1) BR9101206A (de)
CA (1) CA2039317C (de)
DE (1) DE69100074T2 (de)
ES (1) ES2040605T3 (de)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0541105A2 (de) * 1991-11-06 1993-05-12 Praxair Technology, Inc. Verbrennungsverfahren mit Rückführungs- und idealer Strömungszone
GB2261938A (en) * 1991-11-29 1993-06-02 Robin Anthony Kyffin Heat treatment of expansible material to form lightweight aggregate
WO1993011084A1 (en) * 1991-11-29 1993-06-10 Robin Anthony Kyffin Heat treatment of expansible materials to form lightweight aggregate
EP0567131A2 (de) * 1992-04-22 1993-10-27 Institute of Gas Technology Verfahren zur mit Sauerstoff angereicherten Verbrennung
EP0653590A1 (de) * 1993-11-17 1995-05-17 Praxair Technology, Inc. Verfahren für stark gestufte Verbrennung
FR2733303A1 (fr) * 1995-04-19 1996-10-25 Gaz De France Chaudiere-incinerateur de dechets et procede de fonctionnement d'une chaudiere-incinerateur de dechets
EP1612482A2 (de) * 2004-06-30 2006-01-04 CENTRO SVILUPPO MATERIALI S.p.A. Abfallentsorgungvorrichtung
DE102006028770A1 (de) * 2006-06-23 2007-12-27 Basf Coatings Ag Verbrennungsanlage für flüssige und feste Rückstände
DE102012002548A1 (de) 2012-02-09 2013-08-14 Linde Aktiengesellschaft Befeuerung eines Drehrohrofens
EP2626628A1 (de) 2012-02-09 2013-08-14 Linde Aktiengesellschaft Befeuerung eines Drehrohrofens
EP2869012A1 (de) * 2013-10-29 2015-05-06 Linde Aktiengesellschaft Verfahren zum Betreiben eines Drehtrommelofens
EP3037765A1 (de) 2014-12-26 2016-06-29 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Direkt befeuerte geneigte Gegenstrom-Drehöfen und Verwendung davon

Families Citing this family (4)

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Publication number Priority date Publication date Assignee Title
KR100339484B1 (ko) * 1999-08-06 2002-05-31 장기종 로터리 킬른 소각 시스템
DE102006023677A1 (de) * 2006-05-19 2007-11-22 Polysius Ag Anlage und Verfahren zur Herstellung von Zementklinker
EP2208935A1 (de) * 2009-01-15 2010-07-21 Siemens Aktiengesellschaft Brennkammer und Gasturbine
JP5876264B2 (ja) * 2011-10-07 2016-03-02 株式会社アクトリー 廃棄物処理装置

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DE2549076A1 (de) * 1975-11-03 1977-05-12 Kraftanlagen Ag Einrichtung zur verbrennung von abfallstoffen
US4245571A (en) * 1978-04-05 1981-01-20 T R Systems, Inc. Thermal reductor system and method for recovering valuable metals from waste
EP0344784A2 (de) * 1988-06-03 1989-12-06 Praxair Technology, Inc. Verbrennungsverfahren mit niedrigem NOx-Gehalt und mit hohem Leistungsgrad
EP0416533A1 (de) * 1989-09-05 1991-03-13 Praxair Technology, Inc. Verbrennungsverfahren mit verbesserter Temperaturverteilung

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JPS5141271A (en) * 1974-09-24 1976-04-07 Daburyuu Baakusu Paa Ekitai gasujo oyobi peesutojohatsubutsunoshokyakuho narabini sochi
JPH0210017A (ja) * 1988-06-29 1990-01-12 Mitsubishi Heavy Ind Ltd ゴミ焼却装置

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2549076A1 (de) * 1975-11-03 1977-05-12 Kraftanlagen Ag Einrichtung zur verbrennung von abfallstoffen
US4245571A (en) * 1978-04-05 1981-01-20 T R Systems, Inc. Thermal reductor system and method for recovering valuable metals from waste
EP0344784A2 (de) * 1988-06-03 1989-12-06 Praxair Technology, Inc. Verbrennungsverfahren mit niedrigem NOx-Gehalt und mit hohem Leistungsgrad
EP0416533A1 (de) * 1989-09-05 1991-03-13 Praxair Technology, Inc. Verbrennungsverfahren mit verbesserter Temperaturverteilung

Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0541105A3 (en) * 1991-11-06 1993-09-01 Praxair Technology, Inc. Recirculation and plug flow combustion method
EP0541105A2 (de) * 1991-11-06 1993-05-12 Praxair Technology, Inc. Verbrennungsverfahren mit Rückführungs- und idealer Strömungszone
GB2276438B (en) * 1991-11-29 1995-04-26 Robin Anthony Kyffin Heat treatment of expansible materials to form lightweight aggregate
GB2261938A (en) * 1991-11-29 1993-06-02 Robin Anthony Kyffin Heat treatment of expansible material to form lightweight aggregate
WO1993011084A1 (en) * 1991-11-29 1993-06-10 Robin Anthony Kyffin Heat treatment of expansible materials to form lightweight aggregate
US5482458A (en) * 1991-11-29 1996-01-09 Kyffin; Robin A. Heat treatment of expansible materials to form lightweight aggregate
GB2276438A (en) * 1991-11-29 1994-09-28 Robin Anthony Kyffin Heat treatment of expansible materials to form lightweight aggregate
EP0567131A3 (en) * 1992-04-22 1993-12-22 Inst Gas Technology Oxygen-enriched combustion method
EP0567131A2 (de) * 1992-04-22 1993-10-27 Institute of Gas Technology Verfahren zur mit Sauerstoff angereicherten Verbrennung
EP0653590A1 (de) * 1993-11-17 1995-05-17 Praxair Technology, Inc. Verfahren für stark gestufte Verbrennung
JPH07198109A (ja) * 1993-11-17 1995-08-01 Praxair Technol Inc 深段階的燃焼法
KR100252332B1 (ko) * 1993-11-17 2000-05-01 조안 엠. 젤사 질소산화물의 생성을 감소시키기 위한 연소방법(method for deeply staged combustion)
US6394790B1 (en) 1993-11-17 2002-05-28 Praxair Technology, Inc. Method for deeply staged combustion
FR2733303A1 (fr) * 1995-04-19 1996-10-25 Gaz De France Chaudiere-incinerateur de dechets et procede de fonctionnement d'une chaudiere-incinerateur de dechets
EP1612482A2 (de) * 2004-06-30 2006-01-04 CENTRO SVILUPPO MATERIALI S.p.A. Abfallentsorgungvorrichtung
EP1612482A3 (de) * 2004-06-30 2006-05-17 CENTRO SVILUPPO MATERIALI S.p.A. Abfallentsorgungvorrichtung
DE102006028770A1 (de) * 2006-06-23 2007-12-27 Basf Coatings Ag Verbrennungsanlage für flüssige und feste Rückstände
DE102006028770B4 (de) * 2006-06-23 2008-04-30 Basf Coatings Ag Verbrennungsanlage für flüssige und feste Rückstände und Verfahren
DE102012002548A1 (de) 2012-02-09 2013-08-14 Linde Aktiengesellschaft Befeuerung eines Drehrohrofens
EP2626628A1 (de) 2012-02-09 2013-08-14 Linde Aktiengesellschaft Befeuerung eines Drehrohrofens
EP2869012A1 (de) * 2013-10-29 2015-05-06 Linde Aktiengesellschaft Verfahren zum Betreiben eines Drehtrommelofens
EP3037765A1 (de) 2014-12-26 2016-06-29 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Direkt befeuerte geneigte Gegenstrom-Drehöfen und Verwendung davon
US10280114B2 (en) 2014-12-26 2019-05-07 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Direct-fired inclined counterflow rotary kilns and use thereof

Also Published As

Publication number Publication date
DE69100074D1 (de) 1993-06-09
EP0451648A3 (en) 1992-05-13
EP0451648B1 (de) 1993-05-05
KR960010601B1 (ko) 1996-08-06
CA2039317C (en) 1995-01-17
KR910017153A (ko) 1991-11-05
JPH04225783A (ja) 1992-08-14
ES2040605T3 (es) 1993-10-16
BR9101206A (pt) 1991-11-05
DE69100074T2 (de) 1993-08-12

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