US3881430A - Two-stage incinerator - Google Patents

Two-stage incinerator Download PDF

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US3881430A
US3881430A US420888A US42088873A US3881430A US 3881430 A US3881430 A US 3881430A US 420888 A US420888 A US 420888A US 42088873 A US42088873 A US 42088873A US 3881430 A US3881430 A US 3881430A
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stage
zone
products
combustion
burner
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US420888A
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Howard M Katz
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Phillips Petroleum Co
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    • 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
    • F23G5/14—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
    • F23G5/16—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion in a separate combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/05—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste oils
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/60—Combustion in a catalytic combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/50—Fluidised bed furnace
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S588/00—Hazardous or toxic waste destruction or containment
    • Y10S588/90—Apparatus

Definitions

  • Fieid 8 28 oils or similar products which are difficult to combust i 4 is accomplished in a two-stage incinerator including a first stage vaporization zone with burner and forced
  • References Cited air supply and a catalyst material Communication is provided between the first stage vaporization zone and UNITED STATES PATENTS a second stage combustion zone with burner and 3,119,378 1/1964 Marshall 122/4 f d air 5 1 3,306,236 2/l967 Campbell llD/S pp y 3.589.313 6/1971 Smith et 1 I018 2 Claims, 2 Drawing Figures FATE N TED HAY 6 I975 FIG.2
  • FIG. 1 A first figure.
  • TWO-STAGE INCINERATOR This invention relates to improvements in the incineration of waste materials. More particularly, the in vention relates to an improved method for combustion of waste materials and to an improved smokeless incinerator.
  • U.S. Pat. No. 3,680,500 relates to a two-stage incinerator.
  • the first stage is a vaporization or volatilization stage achieved by directing a flame from a first burner together with forced air in a generally downward manner to the first stage and onto the upper area or surfaces of the materials to be combusted. Volatile matter is volatilized, some combustion occurs in this chamber and all gaseous products are conducted to a contiguous second stage in which further oxidation and combustion occur through the use of a second burner and a further supply of forced air. While the incinerator described in US. Pat. No.
  • FIG. 1 shows in elevation form the components of the improved incinerator.
  • FIG. 2 is a sectional view showing diagrammatically the construction of the first stage vaporization zone of the improved incinerator.
  • a waste material which is difficult to combust is introduced through chute into first vaporization zone ll.
  • liquid waste materials such as oil/water emulsions or hydrocarbon oils
  • atomizing air or steam can be introduced through injection nozzle 13.
  • the waste materials are subjected to a high rate input of fuel from burner 14.
  • Fuel is directed to a pilot light on burner 14 through line 15 with the main supply of fuel to the burner being fed through line 16.
  • the fuel which can be any conventional fuel such as gas, fuel oil or the like, is mixed with air or other oxygen-containing gas which is introduced through conduit 18.
  • the combustion gas introduced through conduit 18 is generally, though not necessarily, over and above that necessary for simple combustion of the fuel supply to the burner 14.
  • the forced air supplied through 18 may provide at least partial combustion in the first stage vaporization zone 1 l, but primarily the purpose of the first stage vaporization zone H is to provide a zone of high rate heat input so as to vaporize readily vaporizable components in the waste material to be consumed.
  • the burner 14 is illustratively posed with a generally vertically-directed combustion thrust downwardly toward and onto the waste material which is introduced through chute 10 at a point below the burner.
  • a plurality of burners 14 can be employed in the upper portion of vaporization zone 11.
  • the heavy components in the waste material which are not readily vaporized in zone 11 fall downwardly through vaporization zone 11 and eventually admix with a pelleted catalyst material 20 which is supported on perforated plate or screen 21.
  • a gas such as air is introduced through conduit 22, controlled by pressure control valve 26, passed upwardly through air tubes 23 and through perforated plate 21 to at least partially fluidize the catalyst particles 20.
  • the heavy waste material which accumulates in the catalyst bed 20 is partially burned with the underfire air, and also, in the case of heavier hydrocarbons, it is cracked into lighter, more vaporizable components.
  • the catalyst 20 can be any suitable catalyst known to be useful for cracking hydrocarbons.
  • Representative catalysts are activated clay, synthetic gels, such as silica-alumina, silica-zirconia, alumina-boria, silica-magnesia, and particularly the natural and synthetic zeolite materials, more particularly the synthetic materials commonly termed molecular sieves, all well known in the cracking art.
  • the catalyst may be in the form of pellets, wafers, cylinders and the like. Particle size of the catalyst is not critical and can range from about I /32 inch diameter to inch diameter, or larger, preferably 1/ l 6 inch to inch diameter if pellets are used. Corresponding sizes of other catalyst particle shapes may be used.
  • All gaseous products including products of combustion of the fuel, excess air, vaporized waste and any products of partial combustion in the first vaporization zone 11 form a gaseous stream which is conducted by confined conduit 25 to the second stage 28 combustion zone wherein primary oxidative combustion takes place.
  • the second stage combustion zone 28 fuel is admitted to burner means 29 together with additional and preferably preheated forced air or oxygen-containing gas introduced through line 30.
  • This forced air is considerably in excess of that necessary for combustion purposes.
  • One or more burners 29 can be utilized, two such being shown in the drawing.
  • All vaporized, oxidizable components received in the second stage combustion zone 28 are fully combusted therein, that is, oxidized as fully as possible, and exit from the combustion zone through conduit 31.
  • the second stage combustion zone 28 is preferably equipped near its outlet with quench air inlet means 32, single or multiple, so that the temperature of the hot gases is sharply reduced by mixing with relatively large quantities of relatively cool ambient air. The temperature reduction can be controlled within a wide range, depending on relative temperatures and volumes of the hot gases and the quench air.
  • the final exit gases are essentially smokeless and exit the system through stack 34.
  • a highly refractory protective lining designated by numeral 24 is placed within each of the zones ll and 28 and the closed conduit 25 between said zones, and to the extent necessary within exit line 31 and stack means 34.
  • the employment of quench air at the exit of the second stage combustion zone 28 radically cools the exiting gases to a degree more compatible for simpler disposal and reduces quite sharply the insulative requirements of the stack means 34.
  • the temperature reached or maintained in the first vaporization zone 11 and the second combustion zone 28 will depend upon the materials to be combusted and can reach elevated temperatures of l,50() to 2,400 F.
  • first stage vaporization zone or more in the first stage vaporization zone and equiva lently even higher in the second stage oxidative combustion zone.
  • the respective temperatures in the first stage and the second stage can be regulated by the respective degree or extent of fuel or air introduced to each burner therein and for fluidizing purposes. More easily volatilized components or materials in the first stage vaporization zone containing the cracking catalyst can be volatilized at lower temperatures, with primary combustion then controlled to occur in the second stage oxidative combustion zone. More difiiculty volatilizable materials, of course, may require even higher temperatures in the first stage vaporization zone.
  • volume ratio of first zone to second zone of approximately 1:3.
  • a volume ratio of about l:2.5 may be considered as being a preferred minimum, 1:3 as being more preferred, and the ratio may extend upwardly to as much as 1:6 where additional volume in the second stage and stack are desired or when required by legal restrictions concerning stack sizes and heights.
  • the improved incinerator and method of this invention are particularly adapted for incineration of heavy hydrocarbon oils and oil/water emulsions which are ordinarily resistant to combustion.
  • the presence of the cracking catalyst in the first vaporization zone causes cracking of the heavy components which accumulate therein to form more easily vaporizable materials. Because of this, less auxiliary fuel, shorter residence times and lower temperatures are required in vaporization zone 11.
  • Any residue remaining on top of or intermingled with the catalyst can be periodically removed by providing access thereto.
  • the cracking catalyst can be periodically regenerated by stopping the introduction of waste material into zone ll and permitting upwardly flowing air to contact the catalyst.
  • the exterior casing of elements 10, ll, 25 and 28 is metal represented by numeral 36.
  • the burners useful in the first and second stages of the incinerator of this invention can be any suitable high combustion rate burners. Where disposal of waste gases additionally is desired, that is, in addition to or in conjunction with the aforedescribed liquid wastes, specialized burners such as described in US. Pat. No. 2,753,925, Campbell et al., are useful in that while my incinerator incinerates liquid wastes, such burners incinerate the waste gases.
  • a two-stage contiguous incinerator comprising:
  • a first stage comprising a vaporization zone, at least one first burner, at least one forced air supply, inlet for waste materials, outlet for gaseous products,
  • a second stage comprising a combustion zone, at least one second burner, at least one second forced air supply, entrance for receiving gaseous products from said first stage, outlet for combusted gaseous products from said second stage,
  • a method of incinerating waste products comprising the steps of:
  • step (c) exhausting the products of oxidative combustion from said step (c) to the atmosphere.

Abstract

Incineration of waste products such as hydrocarbon oils or similar products which are difficult to combust is accomplished in a two-stage incinerator including a first stage vaporization zone with burner and forced air supply and a catalyst material. Communication is provided between the first stage vaporization zone and a second stage combustion zone with burner and forced air supply.

Description

O United States Patent 1191 1111 3,881,430 Katz May 6, 1975 TWO-STAGE INCINERATOR 3,680,500 8/1972 110/8 3,702,595 11/1972 M 'rhe d t l. l10/28 [75] Ward Bartlesvlne' Okla 3.759936 9 1973 wil ie 48/209 [73] Assignee: Phillips Petroleum Company,
Bafilesville, Okla- Primary Examiner-Kenneth W. Sprague Attorney, Agent, or Firm-Neuman, Williams, 22 l d. 1 8 Dec 1973 Anderson & Olson [2|] Appl. No.: 420,888
[57] ABSTRACT 3 110/8 Incineration of waste products such as hydrocarbon [58] Fieid 8 28 oils or similar products which are difficult to combust i 4 is accomplished in a two-stage incinerator including a first stage vaporization zone with burner and forced [56] References Cited air supply and a catalyst material. Communication is provided between the first stage vaporization zone and UNITED STATES PATENTS a second stage combustion zone with burner and 3,119,378 1/1964 Marshall 122/4 f d air 5 1 3,306,236 2/l967 Campbell llD/S pp y 3.589.313 6/1971 Smith et 1 I018 2 Claims, 2 Drawing Figures FATE N TED HAY 6 I975 FIG.2
FIG.
TWO-STAGE INCINERATOR This invention relates to improvements in the incineration of waste materials. More particularly, the in vention relates to an improved method for combustion of waste materials and to an improved smokeless incinerator.
U.S. Pat. No. 3,680,500 relates to a two-stage incinerator. The first stage is a vaporization or volatilization stage achieved by directing a flame from a first burner together with forced air in a generally downward manner to the first stage and onto the upper area or surfaces of the materials to be combusted. Volatile matter is volatilized, some combustion occurs in this chamber and all gaseous products are conducted to a contiguous second stage in which further oxidation and combustion occur through the use of a second burner and a further supply of forced air. While the incinerator described in US. Pat. No. 3,680,500 effectively achieves incineration of various waste materials, it has now been found that even more effective incineration of materials, particularly difficultly combustible liquid waste materials, can be accomplished. Oil/water emulsions, heavy hydrocarbon oils and similar materials are hard to incinerate due to high water and carbon contents which require long residence time at high temperatures to achieve complete combustion. The improved incinerator and the incineration method of the present invention effectively accomplish substantially complete combustion of such difficulty combustible waste materials.
The improved incinerator and process of this invention will be discussed in further detail in conjunction with the drawings wherein:
FIG. 1 shows in elevation form the components of the improved incinerator.
FIG. 2 is a sectional view showing diagrammatically the construction of the first stage vaporization zone of the improved incinerator.
Thus, referring to the drawings, a waste material which is difficult to combust is introduced through chute into first vaporization zone ll. In the case of liquid waste materials, such as oil/water emulsions or hydrocarbon oils, such materials can be introduced by means of injection nozzle 12. Similarly, atomizing air or steam can be introduced through injection nozzle 13. In the vaporization zone ll, the waste materials are subjected to a high rate input of fuel from burner 14. Fuel is directed to a pilot light on burner 14 through line 15 with the main supply of fuel to the burner being fed through line 16. The fuel, which can be any conventional fuel such as gas, fuel oil or the like, is mixed with air or other oxygen-containing gas which is introduced through conduit 18. The combustion gas introduced through conduit 18 is generally, though not necessarily, over and above that necessary for simple combustion of the fuel supply to the burner 14. The forced air supplied through 18 may provide at least partial combustion in the first stage vaporization zone 1 l, but primarily the purpose of the first stage vaporization zone H is to provide a zone of high rate heat input so as to vaporize readily vaporizable components in the waste material to be consumed. The burner 14 is illustratively posed with a generally vertically-directed combustion thrust downwardly toward and onto the waste material which is introduced through chute 10 at a point below the burner. A plurality of burners 14 can be employed in the upper portion of vaporization zone 11.
The heavy components in the waste material which are not readily vaporized in zone 11 fall downwardly through vaporization zone 11 and eventually admix with a pelleted catalyst material 20 which is supported on perforated plate or screen 21. A gas such as air is introduced through conduit 22, controlled by pressure control valve 26, passed upwardly through air tubes 23 and through perforated plate 21 to at least partially fluidize the catalyst particles 20. The heavy waste material which accumulates in the catalyst bed 20 is partially burned with the underfire air, and also, in the case of heavier hydrocarbons, it is cracked into lighter, more vaporizable components. The catalyst 20 can be any suitable catalyst known to be useful for cracking hydrocarbons. Representative catalysts are activated clay, synthetic gels, such as silica-alumina, silica-zirconia, alumina-boria, silica-magnesia, and particularly the natural and synthetic zeolite materials, more particularly the synthetic materials commonly termed molecular sieves, all well known in the cracking art. The catalyst may be in the form of pellets, wafers, cylinders and the like. Particle size of the catalyst is not critical and can range from about I /32 inch diameter to inch diameter, or larger, preferably 1/ l 6 inch to inch diameter if pellets are used. Corresponding sizes of other catalyst particle shapes may be used. All gaseous products, including products of combustion of the fuel, excess air, vaporized waste and any products of partial combustion in the first vaporization zone 11 form a gaseous stream which is conducted by confined conduit 25 to the second stage 28 combustion zone wherein primary oxidative combustion takes place.
in the second stage combustion zone 28, fuel is admitted to burner means 29 together with additional and preferably preheated forced air or oxygen-containing gas introduced through line 30. This forced air is considerably in excess of that necessary for combustion purposes. One or more burners 29 can be utilized, two such being shown in the drawing. All vaporized, oxidizable components received in the second stage combustion zone 28 are fully combusted therein, that is, oxidized as fully as possible, and exit from the combustion zone through conduit 31. The second stage combustion zone 28 is preferably equipped near its outlet with quench air inlet means 32, single or multiple, so that the temperature of the hot gases is sharply reduced by mixing with relatively large quantities of relatively cool ambient air. The temperature reduction can be controlled within a wide range, depending on relative temperatures and volumes of the hot gases and the quench air. The final exit gases are essentially smokeless and exit the system through stack 34.
A highly refractory protective lining designated by numeral 24 is placed within each of the zones ll and 28 and the closed conduit 25 between said zones, and to the extent necessary within exit line 31 and stack means 34. The employment of quench air at the exit of the second stage combustion zone 28 radically cools the exiting gases to a degree more compatible for simpler disposal and reduces quite sharply the insulative requirements of the stack means 34.
The temperature reached or maintained in the first vaporization zone 11 and the second combustion zone 28 will depend upon the materials to be combusted and can reach elevated temperatures of l,50() to 2,400 F.
or more in the first stage vaporization zone and equiva lently even higher in the second stage oxidative combustion zone. The respective temperatures in the first stage and the second stage can be regulated by the respective degree or extent of fuel or air introduced to each burner therein and for fluidizing purposes. More easily volatilized components or materials in the first stage vaporization zone containing the cracking catalyst can be volatilized at lower temperatures, with primary combustion then controlled to occur in the second stage oxidative combustion zone. More difiiculty volatilizable materials, of course, may require even higher temperatures in the first stage vaporization zone.
lt presently appears to be preferable to operate with a volume ratio of first zone to second zone of approximately 1:3. A volume ratio of about l:2.5 may be considered as being a preferred minimum, 1:3 as being more preferred, and the ratio may extend upwardly to as much as 1:6 where additional volume in the second stage and stack are desired or when required by legal restrictions concerning stack sizes and heights.
The improved incinerator and method of this invention are particularly adapted for incineration of heavy hydrocarbon oils and oil/water emulsions which are ordinarily resistant to combustion. The presence of the cracking catalyst in the first vaporization zone causes cracking of the heavy components which accumulate therein to form more easily vaporizable materials. Because of this, less auxiliary fuel, shorter residence times and lower temperatures are required in vaporization zone 11.
Any residue remaining on top of or intermingled with the catalyst can be periodically removed by providing access thereto. The cracking catalyst can be periodically regenerated by stopping the introduction of waste material into zone ll and permitting upwardly flowing air to contact the catalyst.
The exterior casing of elements 10, ll, 25 and 28 is metal represented by numeral 36.
The burners useful in the first and second stages of the incinerator of this invention can be any suitable high combustion rate burners. Where disposal of waste gases additionally is desired, that is, in addition to or in conjunction with the aforedescribed liquid wastes, specialized burners such as described in US. Pat. No. 2,753,925, Campbell et al., are useful in that while my incinerator incinerates liquid wastes, such burners incinerate the waste gases.
Those modifications and equivalents which fall within the spirit of the invention are to be considered a part thereof.
What is claimed is:
1. A two-stage contiguous incinerator comprising:
a. a first stage comprising a vaporization zone, at least one first burner, at least one forced air supply, inlet for waste materials, outlet for gaseous products,
b. a bed of catalyst within said vaporization zone,
c. a second stage comprising a combustion zone, at least one second burner, at least one second forced air supply, entrance for receiving gaseous products from said first stage, outlet for combusted gaseous products from said second stage,
d. connecting conduit for conducting vaporous products from said first stage to said second stage by confined means.
2. A method of incinerating waste products comprising the steps of:
a. vaporizing vaporizable components of said waste products in a first stage zone in the presence of a fluidized bed of cracking catalyst,
b. conducting said vaporized components from said step (a) by confined means to a second stage,
c. oxidatively combusting said vaporized components in said second stage in the presence of excess oxygen at an elevated temperature, and
d. exhausting the products of oxidative combustion from said step (c) to the atmosphere.

Claims (2)

1. A two-stage contiguous incinerator comprising: a. a first stage comprising a vaporization zone, at least one first burner, at least one forced air supply, inlet for waste materials, outlet for gaseous products, b. a bed of catalyst within said vaporization zone, c. a second stage comprising a combustion zone, at least one second burner, at least one second forced air supply, entrance for receiving gaseous products from said first stage, outlet for combusted gaseous products from said second stage, d. connecting conduit for conducting vaporous products from said first stage to said second stage by confined means.
2. A method of incinerating waste products comprising the steps of: a. vaporizing vaporizable components of said waste products in a first stage zone in the presence of a fluidized bed of cracking catalyst, b. conducting said vaporized components from said step (a) by confined means to a second stage, c. oxidatively combusting said vaporized components in said second stage in the presence of excess oxygen at an elevated temperature, and d. exhausting the products of oxidative combustion from said step (c) to the atmosphere.
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Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4036153A (en) * 1975-07-03 1977-07-19 Dorr-Oliver Incorporated Fluid bed incinerator feed system
US4095534A (en) * 1977-02-16 1978-06-20 Foster Wheeler Energy Corporation Damper with curved extension plates for wide range flow control
US4277362A (en) * 1977-06-29 1981-07-07 Kernforschungsanlage Julich Gesellschaft Mit Beschrankter Haftung Method of treating radioactively contaminated solvent waste
US4337711A (en) * 1980-09-22 1982-07-06 Clifford Bolton Method for combustion of petroleum and solid wastes
US4838184A (en) * 1988-05-23 1989-06-13 John Zink Company Method and apparatus for disposing of landfill produced pollutants
US5156098A (en) * 1992-01-06 1992-10-20 William W. Bailey Two chamber burner apparatus for destroying waste liquids
US5365864A (en) * 1993-11-02 1994-11-22 Southwest Research Institute Laboratory scale incinerator simulation system
US5550311A (en) * 1995-02-10 1996-08-27 Hpr Corporation Method and apparatus for thermal decomposition and separation of components within an aqueous stream
GB2270503B (en) * 1992-09-11 1996-10-16 Heidelberger Druckmasch Ag Cleaning and waste disposal system of a printing press
US5601040A (en) * 1995-01-09 1997-02-11 Mcgill; Eugene C. Landfill leachate, gas and condensate disposal system
US5934207A (en) * 1997-03-06 1999-08-10 Echols; Richard L. Method and apparatus for disposing of leachate
EP1103458A1 (en) * 1999-11-26 2001-05-30 Yi-Jun Wu Sea-going vessel with a solid-waste incinerator
US20070172784A1 (en) * 2006-01-24 2007-07-26 George Stephens Dual fuel gas-liquid burner
US20070172783A1 (en) * 2006-01-24 2007-07-26 George Stephens Dual fuel gas-liquid burner
US20070172785A1 (en) * 2006-01-24 2007-07-26 George Stephens Dual fuel gas-liquid burner
US20080257806A1 (en) * 2005-09-15 2008-10-23 Silvano Rossato Method and Apparatus for Treating Wastes, Particularly of a Biological and Domestic Origin
BE1018137A3 (en) * 2007-03-20 2010-06-01 Goemans Marcel Gerardus Edmond Liquid, pasty and solid organic residues processing device, has combustion chamber equipped with burner and air injection system, where injection lance provides necessary pressure drop for achieving processing of residues

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US3589313A (en) * 1968-08-30 1971-06-29 Us Health Education & Welfare Solid waste disposal method and apparatus
US3680500A (en) * 1970-10-08 1972-08-01 Phillips Petroleum Co Two-stage smokeless incinerator
US3702595A (en) * 1971-02-04 1972-11-14 Power Gas Ltd Fluidised bed incinerators
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US3119378A (en) * 1956-06-26 1964-01-28 Combustion Eng Steam generation
US3306236A (en) * 1964-09-11 1967-02-28 Exxon Research Engineering Co Burner for waste materials and method of burning waste materials
US3589313A (en) * 1968-08-30 1971-06-29 Us Health Education & Welfare Solid waste disposal method and apparatus
US3759036A (en) * 1970-03-01 1973-09-18 Chevron Res Power generation
US3680500A (en) * 1970-10-08 1972-08-01 Phillips Petroleum Co Two-stage smokeless incinerator
US3702595A (en) * 1971-02-04 1972-11-14 Power Gas Ltd Fluidised bed incinerators

Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4036153A (en) * 1975-07-03 1977-07-19 Dorr-Oliver Incorporated Fluid bed incinerator feed system
US4095534A (en) * 1977-02-16 1978-06-20 Foster Wheeler Energy Corporation Damper with curved extension plates for wide range flow control
US4277362A (en) * 1977-06-29 1981-07-07 Kernforschungsanlage Julich Gesellschaft Mit Beschrankter Haftung Method of treating radioactively contaminated solvent waste
US4337711A (en) * 1980-09-22 1982-07-06 Clifford Bolton Method for combustion of petroleum and solid wastes
US4838184A (en) * 1988-05-23 1989-06-13 John Zink Company Method and apparatus for disposing of landfill produced pollutants
US5156098A (en) * 1992-01-06 1992-10-20 William W. Bailey Two chamber burner apparatus for destroying waste liquids
GB2270503B (en) * 1992-09-11 1996-10-16 Heidelberger Druckmasch Ag Cleaning and waste disposal system of a printing press
US5365864A (en) * 1993-11-02 1994-11-22 Southwest Research Institute Laboratory scale incinerator simulation system
US5601040A (en) * 1995-01-09 1997-02-11 Mcgill; Eugene C. Landfill leachate, gas and condensate disposal system
US5550311A (en) * 1995-02-10 1996-08-27 Hpr Corporation Method and apparatus for thermal decomposition and separation of components within an aqueous stream
US5934207A (en) * 1997-03-06 1999-08-10 Echols; Richard L. Method and apparatus for disposing of leachate
EP1103458A1 (en) * 1999-11-26 2001-05-30 Yi-Jun Wu Sea-going vessel with a solid-waste incinerator
US20080257806A1 (en) * 2005-09-15 2008-10-23 Silvano Rossato Method and Apparatus for Treating Wastes, Particularly of a Biological and Domestic Origin
US20070172784A1 (en) * 2006-01-24 2007-07-26 George Stephens Dual fuel gas-liquid burner
US20070172783A1 (en) * 2006-01-24 2007-07-26 George Stephens Dual fuel gas-liquid burner
US20070172785A1 (en) * 2006-01-24 2007-07-26 George Stephens Dual fuel gas-liquid burner
WO2007087032A1 (en) * 2006-01-24 2007-08-02 Exxonmobil Chemical Patents Inc. Dual fuel gas-liquid burner
GB2449580A (en) * 2006-01-24 2008-11-26 Exxonmobil Chem Patents Inc Dual fuel gas-liquid burner
GB2449580B (en) * 2006-01-24 2009-10-14 Exxonmobil Chem Patents Inc Dual fuel gas-liquid burner
US7901204B2 (en) 2006-01-24 2011-03-08 Exxonmobil Chemical Patents Inc. Dual fuel gas-liquid burner
US7909601B2 (en) 2006-01-24 2011-03-22 Exxonmobil Chemical Patents Inc. Dual fuel gas-liquid burner
US8075305B2 (en) 2006-01-24 2011-12-13 Exxonmobil Chemical Patents Inc. Dual fuel gas-liquid burner
BE1018137A3 (en) * 2007-03-20 2010-06-01 Goemans Marcel Gerardus Edmond Liquid, pasty and solid organic residues processing device, has combustion chamber equipped with burner and air injection system, where injection lance provides necessary pressure drop for achieving processing of residues

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