EP0748983A1 - Un dispositif pour l'incinération d'ordures ménagères avec dépoussiérage et écaitement de combinaisons acides, particulièrement HC1 - Google Patents

Un dispositif pour l'incinération d'ordures ménagères avec dépoussiérage et écaitement de combinaisons acides, particulièrement HC1 Download PDF

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Publication number
EP0748983A1
EP0748983A1 EP96200757A EP96200757A EP0748983A1 EP 0748983 A1 EP0748983 A1 EP 0748983A1 EP 96200757 A EP96200757 A EP 96200757A EP 96200757 A EP96200757 A EP 96200757A EP 0748983 A1 EP0748983 A1 EP 0748983A1
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Prior art keywords
combustion chamber
gases
basic material
incineration plant
combustion
Prior art date
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Application number
EP96200757A
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German (de)
English (en)
Inventor
Luis Emilio Frontini
Francesco Repetto
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Leonardo SpA
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Finmeccanica SpA
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Publication date
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Publication of EP0748983A1 publication Critical patent/EP0748983A1/fr
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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
    • 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
    • F23G5/006—General arrangement of incineration plant, e.g. flow sheets
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J7/00—Arrangement of devices for supplying chemicals to fire
    • 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
    • F23G2202/102—Combustion in two or more stages with supplementary heating
    • 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
    • F23G2202/103—Combustion in two or more stages in separate chambers
    • 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
    • F23G2202/104—Combustion in two or more stages with ash melting stage
    • 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
    • F23G2202/106—Combustion in two or more stages with recirculation of unburned solid or gaseous matter into 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
    • F23G2203/20—Rotary drum furnace
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2207/00—Control
    • F23G2207/10—Arrangement of sensing devices
    • F23G2207/108—Arrangement of sensing devices for hydrocarbon concentration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2207/00—Control
    • F23G2207/60—Additives supply
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2900/00—Special features of, or arrangements for incinerators
    • F23G2900/00001—Exhaust gas recirculation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/30—Halogen; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2217/00—Intercepting solids
    • F23J2217/40—Intercepting solids by cyclones

Definitions

  • the present invention relates to a waste incineration plant with dust collection and removal of the acid compounds, particularly HCl, from the fumes under hot conditions.
  • porlutants must be removed before the fumes are released into the atmosphere, as must also toxic compounds such as dioxins and furans which result from catalytic interactions between the fly ash and acid precursors such as HCl during the cooling of the fumes.
  • European Patent Application No. 94203404.2 filed on 23.11.94 describes, for example, a hot filtration system in which an axial cyclone, or swirler, located immediately downstream of the combustion chamber and upstream of apparatus for recovering heat from the gas, divides the gas flow into a first fraction containing a relatively small quantity of extremely small particles and a second fraction rich in larger particles, which is subjected to a second filtration process and, thus purified, is then used for the recovery of heat from the gases.
  • the heat absorbed in the reactions is obviously taken from the heat evolved in the combustion process and adds to the heat absorbed by the basic compounds in their heating from their initial temperature, close to the ambient temperature, up to the temperature of the gases into which they are injected.
  • a refuse incineration plant in which basic compounds are introduced into the combustion chamber and/or the post-combustion chamber directly or by means of basic burners, for example of the type described in EP-A-0605041 (flame generating burners into which basic compounds in powder form or in solution are injected) and in which an axial cyclone or swirler located immediately downstream of the post-combustion chamber captures a fraction (10-15%) of the gas flow, which is returned to the combustion chamber or the post-combustion chamber, reducing the unburnt materials and utilising the unreacted basic materials.
  • basic burners for example of the type described in EP-A-0605041 (flame generating burners into which basic compounds in powder form or in solution are injected) and in which an axial cyclone or swirler located immediately downstream of the post-combustion chamber captures a fraction (10-15%) of the gas flow, which is returned to the combustion chamber or the post-combustion chamber, reducing the unburnt materials and utilising the unreacted basic materials.
  • the acid compounds which are in gaseous form in the combustion fumes, are salified to a great extent (with conversion yields even of 70%) and assume the solid or liquid state which enables a large proportion thereof to be captured in the axial cyclone together with a considerable quantity of the excess basic material and fly ash.
  • the proportion of the fumes not captured and largely purified of solid particles and acidic compounds proceeds without substantial load losses through the axial cyclone to the heat-recovery boiler and any subsequent heat exchangers where the destruction and removal of the acidic compounds is completed at decreasing temperatures thanks to the remaining basic material in the gases which is at concentrations close to the stoichiometric ratio.
  • the gas fraction captured by the axial cyclone, containing a high concentration of fly ash, salts produced by the neutralisation of the acidic compounds and excess basic material is reintroduced, without filtration, by means of a blower or equivalent means into the combustion chamber and/or post-combustion chamber, where the basic material in the recycled fraction supplements that injected into the basic burner so as to bring its concentration to a much higher value than the stoichiometric ratio while the fly ash undergoes a second combustion process and the salts produced by the neutralisation reaction are concentrated in the solid combustion waste and discharged therewith.
  • a waste incineration plant having a furnace with a grate and two pathways for the gases (also known as a Volund furnace).
  • the combustion chamber 1 houses a movable grate 2 on to which the refuse to be burnt is fed through a loading aperture 3.
  • a blower 4 supplies the combustion chamber with combustion air through the grate 2.
  • Suitable burners initiate the combustion reaction. Partial combustion of the refuse occurs on the grate with excess air.
  • the combustion mixture is conveyed to a rotary drum 5 where combustion is completed with the excess air, possibly with the aid of post-burners which raise the temperature of the solid waste and cause it to vitrify.
  • the solid waste leaving the drum is discharged into a hopper 6 from which it is removed either periodically or continuously by conventional systems.
  • the remaining proportion of the gases from the partial combustion reaction flows through a by pass 7 past the drum 5 to a post-combustion chamber 8 into which the gases leaving the drum 5 also flow.
  • a regulating lock 9 and any other locks, not illustrated, at the inlet and/or outlet of the drum 5 enable the proportions of the gas flows along the two pathways to be controlled.
  • burners located in the top of the combustion chamber or in the post-combustion chamber help to raise and regulate the temperature of the gases in the post-combustion chamber 7 to a value of the order of 950° to 1000°C or more.
  • the hot gases 10 leaving the combustion chamber then pass through heat-recovery apparatus 11, such as a boiler and heat exchangers, and subsequently through apparatus for filtering and removing acid substances, such as scrubbers and electrostatic filters, shown collectively by the block 12.
  • heat-recovery apparatus 11 such as a boiler and heat exchangers
  • apparatus for filtering and removing acid substances such as scrubbers and electrostatic filters, shown collectively by the block 12.
  • the gas leaving the heat recovery apparatus 11 cannot be at a temperature below 200-250°C if condensation and wet acid attack are to be avoided and the filtration or scrubbing assemblies are expensive, bulky and require frequent maintenance.
  • the fly ash transported in the gas constitutes a catalytic substrate for the resynthesis of halogenated organic compounds such as dioxins and furans, which are particularly toxic, the reactions taking place during the cooling of the gas.
  • At least one injection device preferably but not necessarily a basic burner of the type described in EP-A-0605041, for the injection of basic compounds into the combustion chamber and/or post-combustion chamber, an axial cyclone or swirler for capturing a substantial proportion of the solid particles, disposed immediately downstream of the post-combustion chamber, and means for returning the captured solid particles to the combustion chamber and/or post-combustion chamber.
  • a nozzle 161 for injecting basic material, either in powder form or in aqueous dispersion, directly into the combustion gases is located in the top 13 of the combustion chamber of the furnace.
  • the basic material preferably used because of its cheapness is calcium carbonate (CaCO 3 ) ground to a suitable particle size which may be selected within wide limits, from 40 ⁇ to 500 ⁇ and preferably between 50 and 100 ⁇ .
  • the particle size of the material plays an essential role in the salification of the acidic compounds which occurs in heterogeneous conditions (reaction between solid and gas).
  • the finer the particle size the greater the ratio of the surface area to the volume of the solid reagent in contact with the acidic gases in the fumes, increasing the rate of reaction.
  • the optimum particle size for direct injection of CaCO 3 into gases at a temperature of 900-1000°C is between 50 and 100 ⁇ and it is found that such material is readily conveyed by screws and air injectors.
  • a burner 14 of this type supplied with fuel and combustion gas, for example diesel oil and air, develops a flame 15 with a hot nucleus at a relatively high temperature of the order of 1600-1800°C.
  • fuel and combustion gas for example diesel oil and air
  • the burner 14 has a nozzle 16 for the injection of a basic material, in powdered form or in solution, directly into the hot nucleus of the flame 15.
  • the calcining and/or dehydration and the flashing occurs in a very short space of time, of the order of a fraction of a second, while the basic compound is in the hot flame, without dead burning and wastage of the heat energy of the flame which, as well as achieving the calcining, may also contribute to bringing the temperature of the gases to the desired value.
  • an injector 171 or a basic burner 17 of the same type may be installed in a wall of the post-combustion chamber 8, preferably facing the outlet from the drum 5.
  • the salification occurs with a rate of reaction which is linked to the concentrations of the components, the temperature and the physical state of the reactants.
  • the reaction rate is also increased by the high temperature occurring initially.
  • thermodynamic equilibrium of the salification reaction (1) is displaced considerably to the left.
  • the conversion efficiency is of the order of 10%.
  • thermodynamic yield of the reaction (1) is very low at the initial temperature of the process, it is possible to achieve high conversions of the hydrogen chloride if the base CaO is in excess of the stoichiometric ratio of the CaO to HCl.
  • the axial cyclone is constituted by a cylindrical tube 19 with an inlet nozzle 21 which houses a swirler 20 within it.
  • annular tube 22 of a diameter conveniently less than that of the tube 19 and conveniently shaped so as to form a divergent nozzle and a chamber 23 for confining a secondary flow.
  • the swirler 20 by means of its blades, imparts a rotary component of movement to the gas which enters the nozzle 21 in an axial direction.
  • This rotary component gives rise to a centrifugal effect which causes the solid particles transported by the gas flow towards the tube 22 to accumulate mainly in a peripheral layer of the flow.
  • the tube 22 has the effect of dividing the gas flow into two parts: the first part, corresponding to the central section of the flow, enters the tube 22, continuing its axial movement indicated by the arrow 10.
  • the second part, corresponding to the annular portion of the flow is captured between the tube 19 and the tube 22 and conveyed to the confinement chamber 23 from which it is withdrawn by suitable suction means.
  • first fan 24 and duct 240 which convey the captured fraction of the gas (termed the secondary flow below) or part of this to the combustion chamber through the top of the latter, and/or a second fan 25 and duct 250 which convey part or all of the secondary flow to the conveyor grate 2 for the solid waste where it mixes with the combustion air blown in by the blower 4.
  • the secondary flow 26, which is at a high temperature of the order of 1000°C, may be supplemented by cooler, secondary combustion air 27 which lowers its temperature before its input to the fan 25.
  • the fan 25 and also the fan 24 may be rendered superfluous.
  • a fraction of the kinetic load of the secondary flow may be converted into static load which at least partly helps to support the secondary flow towards the combustion chamber.
  • the axial cyclone may conveniently be dimensioned so that the secondary gas flow is about 10% of the total flow and the efficiency of capture of solid particles is of the order of 95%.
  • Figure 2 is a block-schematic diagram showing the quantitative molar balance between the flows into/out of the combustion chamber/post-combustion chamber 29 and the axial cyclone 30 of a plant such as that of Figure 1 and, with several simplifications introduced purely for clarity, enables the operating conditions of the plant to be defined.
  • HCl indicates the molar flow rate of HCl which is formed during the incineration of the waste.
  • CaO indicates the molar flow rate of CaO which is introduced into the combustion chamber through the basic burners and which is assumed to be in unitary stoichiometric ratio with the HCl flow rate.
  • CaO (E) indicates the molar flow rate of CaO which is captured by the axial cyclone 29 and returned to the combustion chamber.
  • CaO(E) represents a flow rate which is in excess of the stoichiometric flow rate and E defines the excess ratio.
  • the flow rate of HCl leaving the combustion chamber is thus given by HCl(1- ⁇ ) and that of CaO by CaO(1- ⁇ +E).
  • the volumetric fraction of the flow captured by the cyclone is termed ⁇ while the fraction of solid particles captured is given by ⁇ and the flow rate of the HCl which is transferred to the heat-recovery boiler is given by HCl(1- ⁇ ).(1- ⁇ ).
  • the CaO fraction transferred to the heat-recovery boiler is given by CaO(1- ⁇ +E)(1- ⁇ ).
  • the excess CaO in the combustion chamber is thus a function of the ratio ⁇ of capture of the solid particles and the destruction yield ⁇ .
  • the excess CaO which forms in the combustion chamber is about 6 which is such as to ensure the yield indicated.
  • the flow to the heat-recovery boiler contains CaO and HCl in the stoichiometric ratio, the HCl concentration having been reduced to less than a third of its initial value.
  • the temperature of the gas falls and hence the destruction of the HCl continues, giving high yields, even of the order of 80% and with minimum formation of deposits, even in the presence of CaO in the stoichiometric ratio.
  • the HCl concentration in the gas is considerably reduced, down to about 6% of the initial value, and may, if necessary, be further reduced in a scrubber of smaller dimensions and at little expense.
  • the maximum conversion yield is thus obtained with the use of a minimum quantity of basic material, substantially equal to the stoichiometric quantity needed.
  • the salt, CaCl 2 formed in the salification of the HCl with CaO has a fusion point of about 774°C and calcium oxide is soluble in CaCl 2 with the formation, at 750°C, of a eutectic mixture containing about 6% CaO.
  • the consumption of CaO is thus rather greater than (about 1.2 times) that given by the stoichiometric ratio.
  • a further aspect of the present invention provides a regulatory system for modulating the molar flow rate of CaCO 3 in dependence on the concentration of the acid substances in the gases, which is proportional to the mass flow rate of the acid substances in the gases.
  • the control In a system such as that described, which operates with excess basic material, contained in a storage volume, or buffer, formed by the combustion chamber, the control cannot ensure that a predetermined ratio of the concentration of the basic material to that of the acid substances is mainted in the gases in real time but it ensures, in the long term, that quantity of the basic material introduced is exactly the stoichiometric quantity required by the reaction for salifying the acid substances (or in a predetermined ratio thereto) and is not in excess.
  • This regulatory system may be achieved in various ways.
  • a probe 50 may detect the concentration of acid substances in the main gas flow leaving the axial cyclone 18.
  • the probe 50 Since the destruction yield ⁇ of acid compounds in the presence of excess base is largely independent of the concentration of the acid substances, the probe 50 provides an indirect indication of the molar flow rate of the acid compounds formed in the combustion chamber.
  • the signal output by the probe 50 is applied to the input of a control unit 51 which generates a control signal for a regulating member, for example a modulating valve 52, which controls the flow of basic material immitted, purely by way of example, from the nozzle 16 or from any other nozzle provided for the injection of the basic material.
  • a control unit 51 which generates a control signal for a regulating member, for example a modulating valve 52, which controls the flow of basic material immitted, purely by way of example, from the nozzle 16 or from any other nozzle provided for the injection of the basic material.
  • a monitoring probe 53 for monitoring the concentration of the basic material may be arranged in the top 13 of the combustion chamber or at any other point therein, as long as it is downstream of the ducts for introducing the recycled basic material.
  • the two regulatory systems may be combined with each other to ensure a very quick dynamic response to variations in acidity and a slower corrective action in dependence on the concentration of the basic material.
  • a further regulatory action which may be carried out independently or together with the preceding actions, relates to the flow rate of the basic material accompanying the gases in their travel downstream of the axial cyclone.
  • the mass flow rate of CaO is determined essentially by ⁇ for high values of E.
  • the desired ratio of HCl to CaO is thus achieved only for a predetermined flow rate of HCl.
  • the capture ratio ⁇ of the cyclone to be variable so that the quantity of CaO released from the axial cyclone can be regulated.
  • control unit 51 controls a servomotor 54 which moves the divergent nozzle axially so as to vary the distribution ratio ⁇ of the axial cyclone.
  • the CaCl 2 which is formed as a mist in the gas in the combustion chamber at high temperature tends to coalesce into droplets which fall under gravity and mix with the incineration waste.
  • a good proportion of the CaCl 2 is thus removed from the plant with the solid waste.
  • the CaCl 2 forms mainly in the solid phase, as a powder, but in any case in limited quantities correlated with the residual HCl concentration, with minimal formation of deposits and scale.
  • the function of the axial cyclone is not only to capture the excess calcium oxide and the calcium chloride.
  • the reduction in the toxic compounds is thus due to the combined effect of the chemical destruction of their acid precursors and the removal of the substrate which supports their renewed synthesis.
  • the axial cyclone of Figure 1 may in practice be constituted by a battery of axial cyclones disposed in parallel and provided with blades whose angles of incidence can be adjusted, there being for example four (as shown schematically in Figure 39) or more.
  • the total flow may then be distributed in a convenient manner in the various flow sections.
  • Figure 1 shows only one preferred embodiment of an incineration plant which uses a Volund furnace.
  • incineration plant of the invention may use other types of furnace.
  • Figure 4 shows an incineration plant according to the present invention which uses a rotary drum furnace.
  • the waste to be incinerated is discharged into a hopper 33 and conveyed by a screw 34 to the inlet of a rotary drum 35.
  • Combustion air is blown into the inlet of the rotary drum through suitable nozzles as shown by the arrow 36.
  • the outlet of the rotary drum 35 is connected to a hopper 37 for receiving and discharging the solid waste, above which is a vertical-axis post-combustion chamber 38.
  • a basic burner 39 burns secondary air and secondary fuel with the formation of a flame 40 and secondary combustion gas which mixes with the primary gas.
  • a nozzle 41 injects a basic material, such as calcium carbonate, into the flame 40 where it is calcined and reacts with the acidic compounds.
  • a basic material such as calcium carbonate
  • a simple injector may be used for injecting the basic material instead of the basic burner 39.
  • the fraction of the gas which is captured by the cyclone 43, and which contains most of the solid particles and the liquid present in the gases, is conveyed through suction ducts 46 to the base of the post-combustion chamber 38 and/or through ducts 47 to the inlet to the rotary drum 35.
  • the recycled fraction of the gas may previously be mixed with all or some of the primary combustion air introduced into the rotary drum or with the secondary combustion air introduced into the post-combustion chamber.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Incineration Of Waste (AREA)
  • Chimneys And Flues (AREA)
EP96200757A 1995-06-12 1996-03-19 Un dispositif pour l'incinération d'ordures ménagères avec dépoussiérage et écaitement de combinaisons acides, particulièrement HC1 Withdrawn EP0748983A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ITMI951242 1995-06-12
IT95MI001242A IT1276701B1 (it) 1995-06-12 1995-06-12 Impianto di incenerimento rifiuti con depolverizzazione a caldo dei fumi e abbattimento a caldo delle sostanze acide dei fumi, in

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EP0748983A1 true EP0748983A1 (fr) 1996-12-18

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EP96200757A Withdrawn EP0748983A1 (fr) 1995-06-12 1996-03-19 Un dispositif pour l'incinération d'ordures ménagères avec dépoussiérage et écaitement de combinaisons acides, particulièrement HC1

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EP (1) EP0748983A1 (fr)
IT (1) IT1276701B1 (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1999006765A1 (fr) * 1997-07-30 1999-02-11 Institute Of Gas Technology Procede de combustion secondaire
EP1312862A3 (fr) * 2001-11-16 2004-09-08 Ecomb Ab Optimisation de combustion
AT513503B1 (de) * 2012-12-21 2014-05-15 Andritz Energy & Environment Gmbh Verbrennungsanlage
CN114130785A (zh) * 2021-11-09 2022-03-04 深圳市能源环保有限公司 一种垃圾焚烧炉的飞灰处理方法
FR3115861A1 (fr) * 2020-11-03 2022-05-06 Cogexyl Energy Chaudière thermique « hybride » à carburant carboné

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3434970A1 (de) * 1984-09-24 1986-10-16 Thermo-Anlagen-Technik Miehe GmbH, 3256 Coppenbrügge Einrichtung zur minderung der feststoffpartikel- und schadstoff-anteile im zwangsgefoerderten abgasstrom aus der verbrennung von kohlenstoffhaltigen feststoffen in einem reaktorbett
DE3741842C1 (en) * 1987-12-10 1989-02-23 Steinmueller Gmbh L & C Method for reducing amounts of the gaseous pollutants SOx, HF and HCl formed during combustion
EP0605041A1 (fr) * 1992-12-29 1994-07-06 FINMECCANICA S.p.A. AZIENDA ANSALDO Dispositif et procédé de destruction thermique de substances acides dans les gaz de fumées
EP0659462A1 (fr) * 1993-12-22 1995-06-28 FINMECCANICA S.p.A. AZIENDA ANSALDO Système pour le depoussierage à chaud des gaz de rejet d'incinérateur et de stations thermiques

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3434970A1 (de) * 1984-09-24 1986-10-16 Thermo-Anlagen-Technik Miehe GmbH, 3256 Coppenbrügge Einrichtung zur minderung der feststoffpartikel- und schadstoff-anteile im zwangsgefoerderten abgasstrom aus der verbrennung von kohlenstoffhaltigen feststoffen in einem reaktorbett
DE3741842C1 (en) * 1987-12-10 1989-02-23 Steinmueller Gmbh L & C Method for reducing amounts of the gaseous pollutants SOx, HF and HCl formed during combustion
EP0605041A1 (fr) * 1992-12-29 1994-07-06 FINMECCANICA S.p.A. AZIENDA ANSALDO Dispositif et procédé de destruction thermique de substances acides dans les gaz de fumées
EP0659462A1 (fr) * 1993-12-22 1995-06-28 FINMECCANICA S.p.A. AZIENDA ANSALDO Système pour le depoussierage à chaud des gaz de rejet d'incinérateur et de stations thermiques

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1999006765A1 (fr) * 1997-07-30 1999-02-11 Institute Of Gas Technology Procede de combustion secondaire
US5937772A (en) * 1997-07-30 1999-08-17 Institute Of Gas Technology Reburn process
EP1312862A3 (fr) * 2001-11-16 2004-09-08 Ecomb Ab Optimisation de combustion
AT513503B1 (de) * 2012-12-21 2014-05-15 Andritz Energy & Environment Gmbh Verbrennungsanlage
AT513503A4 (de) * 2012-12-21 2014-05-15 Andritz Energy & Environment Gmbh Verbrennungsanlage
EP2746661A3 (fr) * 2012-12-21 2017-11-29 Andritz AG Installation de combustion
FR3115861A1 (fr) * 2020-11-03 2022-05-06 Cogexyl Energy Chaudière thermique « hybride » à carburant carboné
CN114130785A (zh) * 2021-11-09 2022-03-04 深圳市能源环保有限公司 一种垃圾焚烧炉的飞灰处理方法
CN114130785B (zh) * 2021-11-09 2022-12-27 深圳能源环保股份有限公司 一种垃圾焚烧炉的飞灰处理方法

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