WO1999029413A1 - Oxydation thermique sans flamme de gaz d'enfouissement - Google Patents

Oxydation thermique sans flamme de gaz d'enfouissement Download PDF

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Publication number
WO1999029413A1
WO1999029413A1 PCT/US1998/025020 US9825020W WO9929413A1 WO 1999029413 A1 WO1999029413 A1 WO 1999029413A1 US 9825020 W US9825020 W US 9825020W WO 9929413 A1 WO9929413 A1 WO 9929413A1
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WO
WIPO (PCT)
Prior art keywords
stream
flare
oxidizer
outlet
gaseous products
Prior art date
Application number
PCT/US1998/025020
Other languages
English (en)
Inventor
Mark R. Holst
Richard J. Martin
John D. Stilger
John T. Schofield
Bradley L. Edgar
Original Assignee
Thermatrix, 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 Thermatrix, Inc. filed Critical Thermatrix, Inc.
Priority to AU16009/99A priority Critical patent/AU1600999A/en
Publication of WO1999029413A1 publication Critical patent/WO1999029413A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/72—Organic compounds not provided for in groups B01D53/48 - B01D53/70, e.g. hydrocarbons
    • 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
    • F23G5/44—Details; Accessories
    • F23G5/46—Recuperation of heat
    • 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
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • 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
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • F23G7/08—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases using flares, e.g. in stacks
    • 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
    • F23C2201/40—Intermediate treatments between stages
    • F23C2201/401—Cooling
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/10—Combustion in two or more stages
    • F23G2202/101—Combustion in two or more stages with controlled oxidant supply
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/10—Combustion in two or more stages
    • F23G2202/105—Combustion in two or more stages with waste supply in stages
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/50—Combustion in a matrix bed combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/20—Waste heat recuperation using the heat in association with another installation
    • F23G2206/203—Waste heat recuperation using the heat in association with another installation with a power/heat generating installation
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/12—Heat utilisation in combustion or incineration of waste
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Definitions

  • This invention relates to the field of treatment of a landfill gas stream.
  • this invention relates to destruction of the organic components of landfill gas stream.
  • Landfills emit a landfill gas stream containing CH4, CO2, other organic compounds, and inorganic compounds due to organic matter in the landfill decomposing.
  • the decomposition process has a beginning period, a steady state middle period, and an ending period.
  • beginning and ending periods each of which lasts for a few years, the landfill gas stream's composition, BTU value, and emission rate frequently are subject to variation and are much lower than at the steady state conditions.
  • middle steady-state period which lasts between 15 and 25 years, the composition (approximately 50% CH4 and 50% C02), BTU value, and flowrate of the landfill gas stream remain nearly constant.
  • the Clean Air Act of 1996 dictates treatments and gas emissions standards for new landfills and more than 300 existing landfills.
  • the CAA has three main criteria for the installation of the landfill gas emission collection and treatment systems: maximum design capacity and maximum rate of the landfill; the presence of criteria pollutants or hazardous air pollutants (HAPs) above certain thresholds; and the presence of an odor problem.
  • Landfills with a capacity of greater than 2.75 million tons or an emission rate that exceeds 50 metric tons per year of non-methane organic constituents are required to have a collection and treatment system.
  • Landfills that emit criteria pollutants or HAPs above the major source threshold are required to have a collection and treatment system.
  • Criteria pollutants include volatile organic compounds, NOX, SO2, and CO.
  • Major source thresholds for criteria pollutants range from 25 to 100 tons per year (tpy) depending on the jurisdiction.
  • the major source thresholds for HAPs are 10 tpy of any single HAP or 25 tpy of total HAPs.
  • Landfills with an odor problem are required to have a collection and treatment system.
  • the odor criteria may be difficult to meet because many compounds have an extremely low odor threshold, with some thresholds being less than 1 ppbv.
  • Flares and prime movers provide the most inexpensive approach for landfill gas treatment.
  • flares when used alone, do not have the required destruction efficiencies in some cases. In other cases, it may be environmentally and economically favorable to recover the energy in the landfill gas by using a prime mover to, for example, generate electricity or provide shaft power.
  • the landfill gas may have constituents that corrode engines.
  • An additional concern with landfill gas collection systems is the generation of leachate streams.
  • Leachates consist of condensed liquids (mostly water) with dissolved inorganic and organic constituents. In many cases, the resulting leachate streams are considered hazardous waste and must be appropriately treated. The most favorable leachate treatment approach utilizes the energy in the landfill gas stream.
  • the claimed invention provides methods and systems for treating a landfill gas stream containing volatile organic compounds from a landfill gas collection system.
  • the landfill gas stream is mixed with an air stream to form a process gas stream.
  • the process gas stream is directed into a preheated flameless thermal oxidizer.
  • the flameless thermal oxidizer oxidizes the volatile organic compounds in the process gas stream to produce a first gaseous products stream.
  • the flameless thermal oxidizers are relatively resistant to corrosion attack, using them to treat the landfill gas stream is a solution to the problem of corrosion.
  • the process gas stream may be treated by a flameless thermal oxidizer/flare system.
  • the process gas stream is partially flamelessly thermally oxidized in the thermal oxidizer to form the first gaseous products stream.
  • the first gaseous products stream is then combusted in a flare to produce a combusted gaseous products stream.
  • the flare may be a separate unit from the flameless oxidizer or may be an integral part of the flameless thermal oxidizer.
  • the flameless thermal oxidizer/flare system includes a) a flameless thermal oxidizer having a matrix bed of solid heat-resistant material ⁇ having an entrance portion, a reaction portion, and an exit surface; a means for maintaining at least the reaction portion of the matrix bed at a temperature above 1400°F; and an inlet for receiving a process gas stream wherein the inlet is in flow communication with the matrix bed entrance portion; and b) a flare having a means for establishing a flame, wherein the flare is an integral part of the flameless oxidizer.
  • the thermal energy (e.g., enthalpy) of the emission from the flameless thermal oxidizer, or the flameless thermal oxidizer/flare system may be used to evaporate a water vapor stream containing organic compounds from a leachate stream. The water vapor stream is then directed through the flameless thermal oxidizer, or the flameless thermal oxidizer/flare system for destruction of the organic compounds therein.
  • Other embodiments of the invention may recuperate some of the thermal energy of the emissions in a boiler to generate electricity or a steam flow. Further embodiments of the invention may have only the boiler recuperating thermal energy from the emissions and a steam flow from the boiler is used to evaporate the leachate stream.
  • Figure 1 shows a schematic diagram of a landfill gas stream being treated by a flameless thermal oxidizer.
  • Figure 2 shows a schematic diagram of landfill gas stream being treated by a flameless thermal oxidizer/flare system.
  • Figure 3 shows a schematic diagram of cross sectional view of a flameless thermal oxidizer/flare system.
  • Figure 4 shows a cross sectional view of another embodiment of a flameless thermal oxidizer/flare system.
  • Figure 5 shows a schematic diagram of a landfill gas stream and a leachate stream being treated with a flameless thermal oxidizer and a leachate evaporator.
  • Figure 6 shows a schematic diagram of a landfill gas stream and a leachate stream being treated with a flameless thermal oxidizer/flare system and a leachate evaporator, with thermal energy from the system emission being used to generate electricity .
  • Figure 7 shows a schematic diagram of a landfill gas stream and a leachate stream being treated with a flameless thermal oxidizer/flare system and a leachate evaporator, with thermal energy from the system emission being used to generate steam.
  • FIG. 1 a schematic is shown of a landfill gas treatment system 10 that flamelessly thermally oxidizes a landfill gas stream 12 in a flameless thermal oxidizer 14 to treat the gas stream 12.
  • an air stream 16 is mixed into the landfill gas stream 12 to form a process gas stream 18 that is delivered to the flameless thermal oxidizer 14.
  • the flowrates of the landfill gas stream 12 and the air stream 16 are controlled in a manner hereinafter described via valves 22 and 24 in the respective streams.
  • the landfill gas stream 12 is substantially flamelessly, thermally oxidized in the flameless thermal oxidizer 14 to form a gaseous products stream 20 that contains the products of the oxidation reaction.
  • the flameless thermal oxidizer 14 typically operates by flamelessly oxidizing gases within a porous bed of matrix heat-resistant material. The oxidation is called "flameless" because it may occur outside the normal premixed fuel/air flammability limits. As flameless thermal oxidizers are relatively resistant to corrosion, they are able to better withstand the corrosion attacks from the compounds being oxidized therein compared to internal combustion engines.
  • Suitable flameless oxidizers for use in the present invention are described in for example U.S. Patent Nos. 4,688,495 (Galloway); 4,823,711 (Kroneberger et al.);
  • Patent Application Serial No. 08/659,579 are incorporated by reference herein in their entireties. Suitable heat- resistant packing materials for the porous matrix bed are also disclosed in these incorporated references.
  • Preferred flameless thermal oxidizers are disclosed in the Martin et al. , Stilger I, Hoist I, Stilger II, Hoist II, and Stilger III patents.
  • the composition of the process gas stream entering the flameless thermal oxidizer is adjusted (e.g., by adjusting the flow rates of the air stream and gas stream) to provide the process gas stream preferably having an equivalence ratio of from about 0.10 to 50.
  • This equivalence ratio range corresponds to the process gas stream having an enthalpy of from about 10 to about 740 BTU/scf, based on the total volume of the process gas stream.
  • the equivalence ratio is defined according to equation 1:
  • ⁇ is the equivalence ratio
  • (Fmoles/O2moles) actual is the actual ratio of moles of fuel to moles of oxygen being fed into the flameless oxidizer
  • (Fmoles/O2moles) stoichiometric is the theoretical ratio of moles of fuel to moles of oxygen needed to fully combust the fuel.
  • the stoichiometric amount of oxygen (as O2) needed to completely combust one mole of methane is 2 moles of oxygen. If in this example, only one mole of oxygen is used per one mole of methane, then the equivalence ratio is 2. If more than the stoichiometric amount of oxygen is used to form the process gas stream the process gas stream is referred to as a "fuel lean process gas stream” and the equivalence ratio is less than 1. If less than the stoichiometric amount of oxygen is used to form the process gas stream the process gas stream is referred to as a "fuel rich process gas stream” and the equivalence ratio is greater than 1.
  • the preferred equivalence ratio depends upon such factors as the type of flameless thermal oxidizer used and the degree of oxidation desired in the flameless thermal oxidizer.
  • the process gas stream preferably has an equivalence ratio of from about 0.10 to about 0.50 and more preferably from about 0.10 to about 0.40.
  • the flameless oxidizer reacts at least 99.0% , preferably at least 99.9% , more preferably at least 99.99% , and even more preferably at least 99.9999%, by weight of reactable materials in the process gas stream into fully oxidized products such as CO2, H2O, HC1, HF, P2O5, and SO2.
  • the equivalence ratio is preferably from about 0.30 to about 0.50 and more preferably from about 0.34 to about 0.40.
  • straight through it is meant flameless thermal oxidizers, such as those disclosed in Martin, et al.
  • the equivalence ratio for a straight through oxidizer results in a fuel lean process gas stream preferably having an enthalpy of from about 30 BTU/scf to about 40 BTU/scf based on the total volume of process gas.
  • the equivalence ratio of the process gas stream is preferably from about 0.10 to about 0.15, and more preferably from about 0.10 to about 0.12.
  • “recuperative” it is meant that the process gas stream after being oxidized is redirected through the matrix bed to recover energy from the process gas stream. The energy can be used for example to heat the incoming process gas stream.
  • a flameless thermal oxidizer is described for example in Stilger I.
  • the equivalence ratio for the recuperative flameless thermal oxidizer results in a fuel lean process gas stream preferably having an enthalpy of from about 10 BTU/scf to about 14 BTU/scf based on the total volume of process gas. If it is desired to only partially oxidize (i.e, less than fully) the process gas stream in a flameless oxidizer, the equivalence ratio of the process gas stream is preferably from about 1.90 to about 50. This equivalence ratio corresponds to a process stream enthalpy of from about 170 BTU/scf to about 740 BTU.
  • the process gas stream preferably has an equivalence ratio of from about 1.9 to about 3.0 and more preferably from about 2.3 to about 2.8. If it is desired to only partially oxidize the process gas stream in a recuperative type flameless thermal oxidizer, the process gas stream preferably has an equivalence ratio of from about 30 to about 50 and more preferably from about 40 to about 50. It is preferable to operate the flameless oxidizer in a manner to partially oxidize the process gas stream when the flameless thermal oxidizer is used in combination with a second combustion device such as a flare, lean burner, waste heat boiler, or another flameless thermal oxidizer.
  • a second combustion device such as a flare, lean burner, waste heat boiler, or another flameless thermal oxidizer.
  • Such a landfill gas treatment system using a flameless oxidizer and flare is shown for example in Figure 2.
  • the process gas stream 18 is treated in a flameless thermal oxidizer/flare system 26 to produce a combusted gaseous products stream 28.
  • the flameless thermal oxidizer/flare system 26 has the flameless thermal oxidizer 14 and a flare 30.
  • the process gas stream 18 is partially oxidized in the flameless thermal oxidizer 14 to produce a gaseous products stream 20a.
  • the gaseous products stream 20a is directed through the flare 30 and combusted in a flame (not shown) by diffusing ambient air 27 into the gaseous products stream 20a to form the combusted gaseous products stream 28.
  • the flameless oxidizer in this embodiment is a recuperative flameless thermal oxidizer.
  • An advantage to the flameless thermal oxidizer/flare system 26 is that it is useful for processing landfill gas streams having variable amounts of BTU/scf loading and/or continuously high (e.g., greater than about 170 BTU/scf) BTU/scf loading.
  • BTU/scf loading varies over time, the gaseous products stream 20a may be combusted by the flare 30 when the process gas stream 18's equivalence ratio results in partial oxidation in the flameless thermal oxidizer.
  • the flare 30 may be operated continuously to ensure complete oxidation.
  • the flameless thermal oxidizer/flare system 26 Another advantage to the flameless thermal oxidizer/flare system is that by not needing to completely oxidize the process gas stream in the flameless thermal oxidizer, lower amounts of oxygen or air can be used in the flameless thermal oxidizer, permitting a smaller flameless thermal oxidizer to be used for a given volumetric flow rate of landfill gas stream to be treated.
  • the flare 30 may be a separate unit located external to the flameless thermal oxidizer, or the flare 30 may be part of the flameless oxidizer as an integral part of the oxidizer.
  • An example of a flameless thermal oxidizer/flare system 26 having an integral flare is shown in Figure 3.
  • the flameless thermal oxidizer/flare system 26 has a flare portion 110 and a flameless thermal oxidizer portion 108.
  • the flameless thermal oxidizer portion 108 has a porous matrix bed 100, contained within a cylindrical wall 126.
  • the flare portion 110 has a flame and a thermal oxidizer/flare system outlet 37 from which a combusted gaseous products stream 28 exits.
  • a landfill gas stream 12 and an air stream 16 are combined to form a process gas stream 18 that is fed into an inlet 154 and into a bottom portion 156 of the flameless thermal oxidizer.
  • the process gas stream 18 flows through the bed 100, and reacts in a reaction portion 158 of the bed 100, that is above the autoignition temperature of the process gas stream 18, to flamelessly oxidize the process gas stream to form a gaseous products stream 20a.
  • the autoignition temperature of the process gas stream is that temperature where spontaneous chain reactions occur between the oxidizable material and oxygen within the gas phase.
  • the process gas stream is oxidized in a reaction wave within the reaction portion 158 of the bed 100.
  • the gaseous products stream 20a flows out of the matrix bed 100 through an exit surface 160 of the bed 100 towards a zone outlet 112.
  • the gaseous products stream 20a exiting the bed 100 serves as a flame fuel stream 114 for the flare portion 110 of the flameless thermal oxidizer/flare system 26.
  • the flame 118 is formed as a result of diffusing an air stream 122 into an outside surface 116 of the flame fuel stream 114.
  • the flame 118 forms because the flame fuel stream is above its autoignition temperature, so that contacting the flame fuel stream with air results in igniting the flame fuel stream 114.
  • the temperature of the flame fuel stream 114 is preferably greater than about 1400°F and more preferably greater than about 1800°F.
  • the air stream 122 is directed to the flame fuel stream by an annular passage 120 defined by the wall 126 and an outside cylindrical wall 128 approximately concentric with the wall 126.
  • other oxidizing agents may be used in place of or in addition to the air stream 122.
  • the walls 126 and 128 may be of other geometric shapes.
  • the flow of the air stream 122 is controlled by dampers 130 at a bottom end 132 of the outside cylindrical wall 128.
  • Other embodiments of the invention may have other means for controlling and/or promoting the air stream 122 flow.
  • the air stream 122 may be optionally preheated. In the shown embodiment, thermal energy from the matrix bed 100 and gaseous products stream 20a is transferred through the wall 126 and to the air stream 122 as it passes over the wall's 126 outside surface 124.
  • the gaseous products stream 20a exiting the bed 100 may optionally be mixed in a mixing zone 102 with a second gaseous products stream 20b through one or more feed lines 104 coming off of a header 106.
  • the second gaseous products stream 20b is preferably a partially combusted process gas stream from one or more flameless thermal oxidizers (not shown).
  • the feed lines 104 extend through the wall 126 and have an outlet 107 in the mixing zone 102. Also one or more flame arrestors may be installed in lines to the header 106 (not shown).
  • the reaction portion 158 of the bed 100 Prior to feeding the process gas stream into the bed 100, the reaction portion 158 of the bed 100 preferably is preheated to above the autoignition temperature of the process gas stream 18.
  • the reaction portion 158 of the bed 100 is preheated by directing a preheating fluid 164 through a preheater fluid inlet 166 and into the bottom portion 156 of the bed 100.
  • the preheating fluid 164 flows through the bed 100, heating the reaction portion 158 to at least about 1400°F, and preferably at least about 1800°F.
  • the preheating fluid 164 is produced by a preheater 168 combusting a preheater fuel stream 170 and a preheater air stream 172.
  • inventions may use a portion of partially combusted gaseous products stream 20a from another flameless thermal oxidizer or a portion of the landfill gas stream 12 for the preheater fuel stream 170. Still further embodiments of the invention may preheat the reaction portion 158 as disclosed in the incorporated references Galloway, Kroneberger et al. , Martin et al. , Stilger I, Hoist I, Stilger II, Hoist II, and Stilger III patents and the U.S. Patent Application Serial No. 08/659,579.
  • the system may optionally have a smaller heat shield 134 and a larger heat shield 136.
  • the small heat shield 134 has an annular shape and radially extends from the wall 126 at the zone outlet 112 and toward the outside wall 128.
  • the larger heat shield 136 has an annular shape that radially extends from the wall 126 to the bottom end 132 of the outside wall 128.
  • the heat shields 134 and 136 reflect heat from the flame 118.
  • Other embodiments of the invention may have other heat shield arrangements or no heat shields at all.
  • the wall 126 may be made of refractory or some other suitable material.
  • a pilot oxidizer fuel stream such as natural gas or methane
  • the flameless thermal oxidizer/flare system 26 may be fed the optional second gaseous products stream 20b through the one or more feed lines 104.
  • Figure 4 shows another embodiment of a flameless thermal oxidizer/flare system 26 where the flare is an integral part of the oxidizer, and energy from the oxidized process gas stream is recovered.
  • Figure 4 like Figure 3, has a flare portion 110 and a flameless thermal oxidizer portion 108.
  • the flameless thermal oxidizer portion 108 has a straight through design, and has a porous matrix bed 100, contained within a cylindrical wall 126. Alternatively, the flameless thermal oxidizer portion 108 can have a recuperative design (not shown).
  • the flare portion 110 has a flame 118 and a thermal oxidizer/flare system outlet 117 from which a combusted gaseous products stream 28 exits.
  • Figure 4 also has a heat exchange device 109 that removes heat or energy from a partially combusted gaseous products stream 20a
  • the flameless thermal oxidizer/flare system 26 in Figure 4 is operated by mixing a landfill gas stream 12 and an air stream 16 to form a process gas stream 18 that is fed into an inlet 154 and into a bottom portion 156 of the flameless thermal oxidizer.
  • the equivalence ratio of the process gas stream in this embodiment is greater than 1.1 and more preferably greater than 1.9.
  • the process gas stream 18 flows through the bed 100, and reacts in a reaction portion 158 of the bed 100 to form the gaseous products stream 20a.
  • the gaseous products stream 20a flows out of the bed and is then cooled with the heat exchange device 109 to form a flame fuel stream 114.
  • the heat exchange device 109 may be connected to other devices such as an evaporator or boiler (not shown) to use the heat that is recovered in the heat exchange device 109.
  • the flame fuel stream may optionally be mixed with a oxidizing agent stream 111, entering through inlet 113, and containing an oxidizing agent such as air or oxygen.
  • the flame fuel stream is then fed through the outlet 37 where ambient air (not shown) diffuses into the flame fuel stream 114 to form a flame 118.
  • the flame fuel stream may be either above, below, or equal to its auto-ignition temperature depending on how the system is operated. If the flame fuel stream is below its autoignition temperature, an ignition device (not shown) may be used to establish the flame.
  • the resulting combusted gaseous products stream 28 may then be released to the atmosphere or redirected to equipment (not shown) for further treatment.
  • the flameless thermal oxidizer may be in flow communication with other combustion devices such as a lean burner, a waste heat boiler, or another flameless thermal oxidizer to completely combust the process gas stream.
  • the temperature of the flameless thermal oxidizer/flare system 26 can be controlled to reduce the total NOx emitted and to reduce the formation of soot and other particulate matter.
  • the flameless thermal oxidizer/flare system 26 can be operated using a straight through flameless oxidizer in an oxygen deficient environment where the reaction temperature is from about 1600 °F to about 2000 °F.
  • the peak temperature of the flame is also reduced.
  • the peak flame temperature is reduced in the range of from about 1100 °F to about 2200 °F. This results in less NOx, soot, and other particulate matter being emitted.
  • Figures 5-7 show other embodiments of the present invention for recovering the thermal energy of gaseous effluents of the flameless thermal oxidizer 14, or the flameless thermal oxidizer/flare system 26 to treat a leachate stream 200 of the landfill gas collection system (not shown).
  • the leachate stream may be for example water (e.g., ground water) that contains for example organic compounds and/or inorganic compounds such as salts or metals found in the earth.
  • the thermal energy recuperation may be performed for example with a leachate evaporator 202.
  • the leachate evaporator 202 receives a high temperature stream into a heating side 204 and receives the leachate stream 200 into an evaporation side 206.
  • the high temperature stream may be any number of streams as discussed below.
  • the thermal energy from the high temperature stream is transferred to the evaporation side 206 and vaporizes the leachate stream 200 into a water vapor stream 208 containing organic compounds.
  • the cooled high-temperature stream and the water vapor stream 208 exit the evaporator 202.
  • the heating side 204 of the evaporator is any suitable heat exchange device that will transfer the heat from the high temperature stream to the leachate stream.
  • the heat exchange device within the evaporator may directly contact (i.e., a "contact” evaporator) the high temperature stream with the leachate stream, or indirectly contact (i.e., a "non-contact” evaporator) the high temperature stream with the leachate stream.
  • the heat exchange device is preferably non-contacting, such as a heat exchange tube. If the high temperature stream is steam, then the heat exchange device may be either contacting (such as a spray), or noncontacting.
  • an embodiment of the invention may recuperate the thermal energy of the gaseous products stream 20 from the flameless thermal oxidizer 14 by directing the stream 20 through the heating side 204 of a leachate evaporator 202 that is non-contacting.
  • the leachate evaporator separates water and volatile organic compounds from the leachate stream to form a water vapor stream 208.
  • the water vapor stream 208 is directed into the flameless thermal oxidizer 14 for flameless thermal oxidization of the organic compounds therein.
  • the residual nonvolatile compounds from the leachate stream exit the evaporator in an inorganic waste stream 207 and the cooled gaseous products stream 210 is released to the atmosphere or further treated (not shown).
  • Other embodiments of the invention may substitute the flameless thermal oxidizer/flare system 26 for the flameless thermal oxidizer 14 in the embodiment shown in Figure 5.
  • an embodiment of the invention may recuperate the thermal energy of the combusted process gas stream 28 from the flameless thermal oxidizer/flare system 26 by directing the stream 28 through a boiler 212 and the heating side 204 of the leachate evaporator 202 that is noncontacting.
  • the combusted gaseous product stream 28 is directed through a heating manifold 214 in the boiler 212 to transfer thermal energy to the boiler 212 from the stream 28.
  • the post- boiler process gas stream 216 is directed through the heating side 204 of the non-contact leachate evaporator 202.
  • the resulting water vapor stream 208 is directed into the flameless thermal oxidizer/flare system 26 for the organic compounds in the stream 208 to be processed therein.
  • the cooled post-boiler process gas stream 218 is released to the atmosphere or further treated (not shown).
  • the boiler 212 may optionally be connected to a steam turbine 220 to produce power 222 using a boiler steam flow 224.
  • the steam turbine returns a condensate stream 226 back to the boiler 212 for conversion back to steam.
  • Other embodiments of the invention may substitute the flameless thermal oxidizer 14 for the flameless thermal oxidizer/flare system 26 in the embodiment shown in Figure 6.
  • Other embodiments of the invention may use the steam flow 224 from the boiler 212 for other purposes (not shown).
  • an embodiment of the invention may recuperate the thermal energy of the combusted process gas stream 28 from the flameless thermal oxidizer/flare system 26 by directing the stream 28 to a boiler 228.
  • the combusted process gas stream 28 is directed into the boiler 228 and the thermal energy is recuperated therefrom using conventional means.
  • the cooled combustion process gas stream 231 is released to the atmosphere or further treated (not shown).
  • the boiler 228 releases a first steam flow 230 that is directed through the heating side 204 of the leachate evaporator 202.
  • the leachate evaporator 202 may be either contact or non- contact.
  • the resulting water vapor stream 208 is directed into the flameless thermal oxidizer/flare system 26.
  • the cooled first steam flow 232 is released to the atmosphere, returned to the boiler, or further processed (not shown).
  • the boiler 228 may optionally release a second steam flow 234 for use in other operations (not shown).
  • Other embodiments of the invention may have a steam turbine functionally connected to the boiler 228 (not shown).
  • Yet other embodiments of the invention may substitute the flameless thermal oxidizer 14 for the flameless thermal oxidizer/flare system 26 shown in Figure 7.
  • the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof and, accordingly, reference should be made to the appended claims, rather than to the foregoing specification, as indicating the scope of the invention.

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  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)

Abstract

L'invention concerne un procédé et un système permettant de traiter un flux de gaz d'enfouissement qui renferme des composés organiques volatils. On utilise une installation d'oxydation thermique sans flamme pour traiter lesdits composés dans le flux considéré, de manière à constituer un premier flux de produits gazeux. Selon une variante, on traite ce flux plus avant à la torche. La torche en question peut être une unité séparée de l'installation d'oxydation thermique, ou bien elle peut en faire partie. Selon d'autres variantes, on récupère l'énergie thermique des émissions de l'installation susmentionnée ou bien des émissions de la torche, afin de produire par exemple de la vapeur ou de l'électricité. L'énergie thermique récupérée peut être utilisée à son tour pour vaporiser de la vapeur d'eau renfermant les composés organiques volatils émanant d'un flux de lixiviats. On peut ensuite acheminer la vapeur d'eau vers l'installation d'oxydation thermique en vue de son traitement.
PCT/US1998/025020 1997-12-08 1998-11-23 Oxydation thermique sans flamme de gaz d'enfouissement WO1999029413A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU16009/99A AU1600999A (en) 1997-12-08 1998-11-23 Flameless thermal oxidization of landfill gas

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US98655097A 1997-12-08 1997-12-08
US08/986,550 1997-12-08

Publications (1)

Publication Number Publication Date
WO1999029413A1 true WO1999029413A1 (fr) 1999-06-17

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AU (1) AU1600999A (fr)
WO (1) WO1999029413A1 (fr)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100374792C (zh) * 2006-05-15 2008-03-12 南京大学 利用垃圾填埋气生产热水的成套装置
CN102252333A (zh) * 2011-05-05 2011-11-23 福建省丰泉环保控股有限公司 利用垃圾填埋气体焚烧降低氮氧化物的方法及其处理系统
US20130095438A1 (en) * 2011-10-18 2013-04-18 Jeffrey J. Grill Regenerative thermal oxidizer for the reduction or elimination of supplemental fuel gas consumption
EP2636951A1 (fr) * 2012-03-07 2013-09-11 Flare Industries, LLC Appareil et procédé de brûlage à la torche de gaz résiduaire
US8535429B2 (en) 2011-10-18 2013-09-17 Clean Energy Renewable Fuels, Llc Caustic scrubber system and method for biogas treatment
US8574888B2 (en) 2011-10-18 2013-11-05 Clean Energy Fuels Corp. Biological H2S removal system and method
US9005337B2 (en) 2011-10-18 2015-04-14 Clean Energy Renewable Fuels, Llc System for the treatment and purification of biogas

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US5643544A (en) * 1995-04-28 1997-07-01 Applied Web Systems, Inc. Apparatus and method for rendering volatile organic compounds harmless
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Publication number Priority date Publication date Assignee Title
US2756121A (en) * 1954-02-08 1956-07-24 Standard Oil Co Oxidation of waste gases
DE1060847B (de) * 1955-10-14 1959-07-09 Dr Johann Heinrich Helberger Verfahren zur katalytischen flammenlosen Verbrennung gasfoermiger und fluessiger organischer Verbindungen
US4418045A (en) * 1980-09-19 1983-11-29 Nippon Shokubai Kagaku Kogyo Co., Ltd. Method for disposal of waste gas and apparatus therefor
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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100374792C (zh) * 2006-05-15 2008-03-12 南京大学 利用垃圾填埋气生产热水的成套装置
CN102252333A (zh) * 2011-05-05 2011-11-23 福建省丰泉环保控股有限公司 利用垃圾填埋气体焚烧降低氮氧化物的方法及其处理系统
CN102252333B (zh) * 2011-05-05 2012-12-26 福建省丰泉环保控股有限公司 利用垃圾填埋气体焚烧降低氮氧化物的方法及其处理系统
US20130095438A1 (en) * 2011-10-18 2013-04-18 Jeffrey J. Grill Regenerative thermal oxidizer for the reduction or elimination of supplemental fuel gas consumption
WO2013059501A1 (fr) * 2011-10-18 2013-04-25 Clean Energy Fuels Corp. Oxydeur thermique régénératif pour réduire ou supprimer une consommation supplémentaire d'un gaz combustible
US8535429B2 (en) 2011-10-18 2013-09-17 Clean Energy Renewable Fuels, Llc Caustic scrubber system and method for biogas treatment
US8574888B2 (en) 2011-10-18 2013-11-05 Clean Energy Fuels Corp. Biological H2S removal system and method
US8669095B2 (en) 2011-10-18 2014-03-11 Clean Energy Fuels Corp. Method for the treatment of process gas for biological H2S removal
US20150024328A1 (en) * 2011-10-18 2015-01-22 Clean Energy Renewable Fuels, Llc Regenerative thermal oxidizer for the reduction or elimination of supplemental fuel gas consumption
US9005337B2 (en) 2011-10-18 2015-04-14 Clean Energy Renewable Fuels, Llc System for the treatment and purification of biogas
EP2636951A1 (fr) * 2012-03-07 2013-09-11 Flare Industries, LLC Appareil et procédé de brûlage à la torche de gaz résiduaire

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