CN1315992A - Waste incineration disposal method - Google Patents

Waste incineration disposal method Download PDF

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Publication number
CN1315992A
CN1315992A CN99810455A CN99810455A CN1315992A CN 1315992 A CN1315992 A CN 1315992A CN 99810455 A CN99810455 A CN 99810455A CN 99810455 A CN99810455 A CN 99810455A CN 1315992 A CN1315992 A CN 1315992A
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CN
China
Prior art keywords
temperature
refuse
vapourizing furnace
roasting kiln
furnace
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Granted
Application number
CN99810455A
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Chinese (zh)
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CN1213128C (en
Inventor
金子正元
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Kinsei Sangyo Co Ltd
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Kinsei Sangyo Co Ltd
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Publication of CN1315992A publication Critical patent/CN1315992A/en
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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
    • F23G5/50—Control or safety arrangements
    • 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
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B18/00—Use of agglomerated or waste materials or refuse as fillers for mortars, concrete or artificial stone; Treatment of agglomerated or waste materials or refuse, specially adapted to enhance their filling properties in mortars, concrete or artificial stone
    • C04B18/04—Waste materials; Refuse
    • C04B18/06—Combustion residues, e.g. purification products of smoke, fumes or exhaust gases
    • C04B18/10—Burned or pyrolised refuse
    • C04B18/108—Burned or pyrolised refuse involving a melting step
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/04—Cyclic processes, e.g. alternate blast and run
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • 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
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/303—Burning pyrogases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L2900/00—Special arrangements for supplying or treating air or oxidant for combustion; Injecting inert gas, water or steam into the combustion chamber
    • F23L2900/07005—Injecting pure oxygen or oxygen enriched air
    • 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
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/143—Feedstock the feedstock being recycled material, e.g. plastics
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/91—Use of waste materials as fillers for mortars or concrete

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Environmental & Geological Engineering (AREA)
  • Materials Engineering (AREA)
  • Ceramic Engineering (AREA)
  • Civil Engineering (AREA)
  • Structural Engineering (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Incineration Of Waste (AREA)
  • Processing Of Solid Wastes (AREA)
  • Coke Industry (AREA)

Abstract

An incineration disposal method for wastes for preventing PCDDs emission and shortening a disposal cycle, wherein wastes are dry-distilled in a gasification furnace and a combustible gas generated is burned in a combustion furnace. Oxygen is supplied to the combustion furnace according to the volume of the combustible gas, while an oxygen volume supplied to the gasification furnace is controlled according to a change in combustion gas combustion temperature so as to regulate the production volume of the combustible gas to keep a combustion furnace temperature at approximately constant one higher than a preset temperature. When a gasification furnace temperature lowers from a maximum temperature to below a PCDDs production temperature after a combustion furnace temperature falls to below the approximately constant temperature, burned residues are immediately taken out from the gasification furnace. Alternatively, while a gasification furnace temperature is falling from the maximum temperature, burned residues are housed in a fusion furnace connected with the gasification furnace. Thereafter, new wastes are charged into the gasification furnace and ignited. The burned residues are heated in the fusion furnace and molten matter is placed into water for quenching to thereby form granulated solid matter.

Description

Waste incineration disposal method
The present invention relates to a kind of incineration treatment method of refuse.
The applicant once put down in 2 years No. 135280 grade at the open communique of Japan's special permission in advance and disclosed the device of a kind of device as refuses such as burning disposal damaged tires.
In this communique disclosed device by the vapourizing furnace of closed structure with constitute with the roasting kiln that this vapourizing furnace is connected by gas passage, in this vapourizing furnace, make a part of trash burning, use this all the other refuses of combustion heat destructive distillation simultaneously, and the inflammable gas that is produced is imported to this roasting kiln make it perfect combustion.Below, explain flow process by described device burning disposal refuse.
By this device burning disposal refuse the time, at first, light the refuse of in the vapourizing furnace of closed structure, packing in advance, make the part burning of this refuse, simultaneously by its remaining refuse of burning destructive distillation.Be directed in the roasting kiln that is located at described vapourizing furnace outside by gas passage through the inflammable gas that described destructive distillation produced.In this roasting kiln, light by supplying with combustion flame to the inflammable gas that is imported into, this inflammable gas takes fire.
When carrying out destructive distillation and can stablize the generation inflammable gas in described vapourizing furnace, then the generation of this inflammable gas also little by little increases, thereupon, as shown in Figure 5, as the temperature T in the described roasting kiln 2The temperature of combustion of this detected inflammable gas also and then rises.In addition, if utilizing the combustion heat energy of self spontaneously to stablize and burn away, inflammable gas makes the interior temperature T of this roasting kiln 2Reach T 2a, then stop to supply with combustion flame.
In described roasting kiln, in roasting kiln, supply with to making the needed oxygen of this inflammable gas perfect combustion according to the amount of the inflammable gas that is imported.Simultaneously, under the state of described inflammable gas perfect combustion, detect the temperature T in the described roasting kiln 2As the temperature of combustion of this inflammable gas, and according to temperature T 2The amount of oxygen supplied with to vapourizing furnace of variation control, adjust amount by the inflammable gas that destructive distillation produced.Its result, in described device, can be the temperature T in the described roasting kiln 2Remain on the temperature T that inflammable gas is spontaneously stable and burn away substantially constant 2aAbove temperature T 2b
In described device, proceed described destructive distillation, the pyrogenous refuse of the energy in vapourizing furnace portion tails off, even then increase the amount of oxygen of supplying with to vapourizing furnace, can not produce the temperature T that makes in the described roasting kiln 2Remain on temperature T substantially constant 2bNecessary inflammable gas.So, the temperature T in the roasting kiln 2Decrease, in vapourizing furnace, stop destructive distillation and the burning and the ashing of refuse.In addition, the temperature in the described vapourizing furnace as T 1Be shown in Fig. 5.
Its result by described device, can stablize the destructive distillation of carrying out described refuse and the perfect combustion of described inflammable gas.Then, wait for the temperature T that described vapourizing furnace is interior 1Become the low temperature of easy processing calcination degree, discharge this calcination from this vapourizing furnace, the new refuse of in this vapourizing furnace, packing into simultaneously, by carrying out such process repeatedly and as one-period, the described refuse of burning disposal continuously.
But in described device, because the calcination in the described vapourizing furnace is a high temperature, institute is so that the interior temperature T of vapourizing furnace 1The degree that fully is reduced to easy this calcination of processing needs for a long time, and to make the processing cycle elongated be disadvantageous.
In addition, in recent years, report was once arranged along with the burning disposal refuse produces dioxins materials.This is because described refuse contains chlorine mostly, when 250-350 ℃ the such refuse of temperature combustion, from refuse free chlorine and since the hydrocarbon that the incomplete combustion of resin generates by generating dioxins materials as the reaction of catalyzer with heavy metal contained in this refuse.In order to prevent to discharge the De dioxin, make the De dioxin thermolysis fully that generates need the time long, and to make the processing cycle elongated be disadvantageous at the described refuse of burning disposal.
The present invention is in order to address the above problem, and its objective is provides a kind of incineration treatment method that can prevent the discharge of dioxin and can shorten the refuse in processing cycle.
To achieve these goals, the incineration treatment method of refuse of the present invention, be to have the refuse of lighting in vapourizing furnace to be packed into and make this part trash burning, make it the incendiary operation by the operation of its all the other refuses of combustion heat destructive distillation with importing to roasting kiln by the incendivity gas that this destructive distillation produced; When this this inflammable gas of roasting kiln internal combustion, supply with its needed oxygen and make this inflammable gas burning of burning according to the amount of the inflammable gas that imports to this roasting kiln to this roasting kiln, simultaneously according to the amount of oxygen of supplying with to this vapourizing furnace by the control of the temperature variation in this roasting kiln of incendiary of this inflammable gas in this roasting kiln and adjust amount by the inflammable gas that this destructive distillation produced, the basic constant temperature of temperature in this roasting kiln remain on the improving one's methods of incinerating method of the refuse more than the specified temperature.
The incinerating method of first kind of refuse of the present invention is characterized in that constituting with the igniting operation by taking out operation.This taking-up operation is along with the refuse in the described vapourizing furnace carries out destructive distillation, the pyrogenous waste part of energy in this vapourizing furnace reduces, temperature in this roasting kiln becomes less than after the described substantially invariable temperature, the operation of directly this burning residue being taken out from vapourizing furnace when top temperature reduces and become less than the temperature that generated dioxin by this refuse when the temperature in this vapourizing furnace; And the igniting operation be after taking out this burning residue from this vapourizing furnace, this vapourizing furnace pack into new refuse and the igniting operation.
Described refuse contains chlorine mostly, when 250 ℃-350 ℃ the such refuse of temperature combustion, is considered to produce above-mentioned De dioxin.In addition, in above-mentioned method of the present invention, along with the described refuse in the described vapourizing furnace carries out destructive distillation, the pyrogenous waste part of energy in this vapourizing furnace reduces, after temperature in can not making described roasting kiln remains on basic constant temperature more than the temperature of described regulation, described refuse becomes direct state of combustion, after temperature in described vapourizing furnace reaches top temperature, begin to reduce, becoming less than when this refuse generates the temperature of dioxin, when for example the temperature in the vapourizing furnace is 200 ℃, take out the burning residue of refuse from described vapourizing furnace at once.
At this moment, do not wait until that described burning residue becomes low temperature fully, the described burning residue of taking-up and the new refuse of packing in vapourizing furnace are lighted a fire from vapourizing furnace, can shorten the processing cycle, in addition, new refuse is not owing to packing into when described vapourizing furnace is cold, so can reduce the needed heat of its burning disposal.
In addition, when described vapourizing furnace takes out burning residue, described refuse has the situation that lingering section can pyrogenous refuse, but because the temperature in the vapourizing furnace is low, can not generate dioxin, can prevent in the dioxin discharging atmosphere.
From the described burning residue that described vapourizing furnace took out,, may become the secondary pollution source for discarded place though can increase volume and weight like this by fixed processing such as concrete, pitches.Yet, use waste treatment method of the present invention, in a single day described burning residue after taking out, vapourizing furnace just is encased in melting furnace.Then, with heating of the heating unit of melting furnace and the described burning residue of fusion, and melts dropped in the water by the chilling solid substance that granulates.
In described burning residue, do not have clean-burning refuse even have, when in described melting furnace, heating, then contain the also complete inorganics of burned kish etc. of described burning residue that does not have clean-burning refuse.Then, make described inorganics fusion by further heating.
Because so-called temperature drops to the degree that does not generate dioxin and is still high temperature, so utilize this high temperature by the easy described burning residue of fusion of heating unit energy at described melting furnace.Then the melts that is melted is like this dropped into and carry out the chilling solid substance of being pulverized and granulate in the water.
Granular like this solid substance for example can be used as the filler that building or building are used.
In addition, in said process, this burning residue is taken out in watering back, the upper strata of the burning residue in vapourizing furnace, can prevent that this burning residue from dispersing.
The incineration treatment method of the described refuse of another kind of the present invention is characterized in that constituting by accommodating operation, solid shape operation and igniting operation.This accommodates operation is along with the refuse in the described vapourizing furnace carries out destructive distillation, the pyrogenous waste part of energy in vapourizing furnace reduces, temperature in this roasting kiln becomes less than behind the described basic constant temperature, when the temperature in this vapourizing furnace when top temperature descends, this burning residue is taken out and is loaded to the melting furnace that is connected with the burning residue conveying end of this vapourizing furnace from this vapourizing furnace; Should solid shape operation be to heat and this burning residue of fusion, and become granular solid substance carrying out chilling in the melts input water by the heating unit that is arranged on this melting furnace; This igniting operation is after this burning residue is taken out from this vapourizing furnace, at pack into new refuse and lighting a fire of this vapourizing furnace.
In the incineration treatment method of above-mentioned refuse, the pyrogenous waste part of energy that carries out in this vapourizing furnace of destructive distillation along with the described refuse in the described vapourizing furnace reduces, temperature in the described roasting kiln can not remain on described specified temperature above basic constant temperature, described refuse and become direct state of combustion, after the temperature in the vapourizing furnace reaches the highest temperature, when beginning to reduce takes out described burning residue Yu the generation temperature of dioxin is irrelevant from described vapourizing furnace.At this moment, may worry that dioxin distributes to atmosphere from described burning residue.But, in the method for the invention described above,, can take out burning residue and be encased in melting furnace from described vapourizing furnace so described dioxin can not distribute also because melting furnace is connected with the burning residue conveying end of described vapourizing furnace.
Therefore, reduce back, this burning residue in abundant high temperature by the treatment process of the invention described above, the interior pyrogenous waste part of energy of described vapourizing furnace, from vapourizing furnace, take out this burning residue, and the new refuse of can in vapourizing furnace, packing into, can shorten the processing cycle.In addition, because new refuse is at vapourizing furnace not pack into when cold, so can lower the needed heat of its burning disposal.
The described burning residue of packing at described melting furnace, identical with the situation of the incineration treatment method of above-mentioned first kind of refuse, by the heating unit heating and melting that is provided with at described melting furnace, then melts is thrown in the water through the chilling solid substance that granulates.
In addition, in above-mentioned of the present invention various incineration treatment methods, carry out fusion reduction fusing point by adding flux in described burning residue and make it easier fusion.And, by adding described solvent, when generating described solid substance, because inorganics is comprised in this flux, so can prevent spilling of objectionable impurities such as heavy metal.
As described flux, can mix use, silicic acid, silicate compound, be the main material that becomes, boric acid, boronic acid compounds with the silicate compound, be material, the alkali metal compound of main component, one or two or more kinds of alkaline earth metal compound with the boronic acid compounds.
As described silicate compound or with the silicate compound is the material of principal constituent, can enumerate silica sand, mountain sand, river sand, silica, diatomite, water glass, Magnesium Silicate q-agent, cullet, clay etc.
Described boric acid can be in orthoboric acid, metaboric acid, tetraboric acid, the boron oxide any.In addition, be that the material of principal constituent can be enumerated orthoboric acid salt, metaborate, tetraborate, biborate, pentaborate, six borates, eight borates, borax, lime borate etc. as described boronic acid compounds or with the boronic acid compounds.
In addition, soda-lime, salt, sodium hydroxide etc. can be enumerated, and unslaked lime, slaked lime, Wingdale etc. can be enumerated as described alkali earth metallic compound as described alkali metal compound.
In addition, when with the described burning residue of incineration treatment method fusion of each refuse of the present invention, making the inflammable gas that destructive distillation produced import to described melting furnace at described roasting kiln incendiary waste gas by the refuse in the described vapourizing furnace, by heating described burning residue, the heating of auxiliary described heating unit can be lowered the cost for this heating unit that turns round.
Be arranged on the heating unit of described melting furnace, can be well heater, also may fuel nozzle etc. combustion unit, when this heating unit was combustion unit, the oxygen of supplying with by this melting furnace to this combustion unit that heat heated carried out boosting, can lower the operating cost of this heating unit.
In addition, in the various incineration treatment methods of the invention described above, available heavy oil etc. are as the fuel of described combustion unit, when importing to described inflammable gas in the described roasting kiln, divide and get a part of inflammable gas, make it condensing and the recovery oil content, simultaneously, can make this oil content the fuel of described combustion unit.In addition,, make it the fuel of the oil content of condensing and recovery, can lower the operating cost of described heating unit as described combustion unit by branch being got a part of described inflammable gas.
Below accompanying drawing is carried out simple explanation.
Fig. 1 is the flowage structure figure of expression one embodiment of the invention.
Fig. 2 represents the flowage structure figure of one embodiment of the invention for the major portion of enlarged view 1.
Fig. 3 for the temperature in the vapourizing furnace of incineration treatment method of expression refuse of the present invention and the temperature of combustion in the roasting kiln at any time to the graphic representation that changes.
Fig. 4 represents the flowage structure figure of another embodiment of the present invention for the major portion of enlarged view 1.
Fig. 5 is that the interior temperature of combustion of interior temperature of the vapourizing furnace of expression incineration treatment method in the past and roasting kiln is at any time to the graphic representation that changes.
Embodiment
Below, with reference to accompanying drawing embodiments of the invention are described in further detail.
The formation of the destructive gasifying incinerating and treating device of the refuse of using embodiments of the invention 1 at first, is described below with reference to Fig. 1 and Fig. 2.
At the used device of present embodiment, as shown in Figure 1, the ash handling plant 4 of the burning residue of the burning ash that the roasting kiln 3 that having packs into is connected with this vapourizing furnace 1 based on the vapourizing furnace 1 of the refuse A of the various mixture of waste of damaged tire, by gas passage 2 and handling is discharged by vapourizing furnace 1 etc. (below, claim calcination).
On vapourizing furnace 1, have and establish the input port 6 that freely openable drops into door 5,6 can put into the refuse A of damaged tire etc. in the vapourizing furnace 1 from the input port.Then, the state in that vapourizing furnace is closed its input port 5 interdicts its inside substantially with the outside.
At the peripheral part of vapourizing furnace 1, have with the isolated water jacket 7 in the inside of vapourizing furnace 1 as its cooling structure.Water jacket 7 is supplied water by not shown feeding apparatus and the inner water yield is remained on the water level of regulation.
The bottom of vapourizing furnace 1 has outstanding downwards truncated cone shape, has ash output hole 9 below the side wall portion 8 of inclined plane shape, this ash output hole opening and discharge calcination in the intact back of the burning disposal of refuse A above ash handling plant 4.A pair of base plate 10a, 10b at this ash output hole of freely openable on the ash output hole 9 are installed on a pair of hinge 11a, the 11b.Base plate 10a, 10b can shake around hinge 11a, 11b easy on and off, shake by this and make ash output hole 9 freely openables.
In side wall portion 8, have the empty chamber 8a isolated with the inside of vapourizing furnace 1.By at the set a plurality of spray nozzle of the gas supply 12 of the inner wall part of vapourizing furnace 1, empty chamber 8a is connected with the inside of vapourizing furnace 1.Connect vapourizing furnace with oxygen feedway 13 at described empty chamber 8a, be connected with oxygen (air) supply source 15 that is constituted by gas blower etc. with oxygen feedway 13 by main oxygen feedway 14 vapourizing furnaces.The control valve 17 of valve actuator 16 its degree of opening of control in vapourizing furnace is provided with on oxygen feedway 13.In this situation, by by comprising the control device that electronic circuit constituted 18 control valve driving mechanisms 16 such as CPU.
In addition, in the lower side of vapourizing furnace 1, the portfire 19 of the refuse A that is packed in the mounting points gasification stove 1, this igniting is controlled by control device 18.Portfire 19 is made of pilot burner etc., by making by main fuel feedway 21, vapourizing furnace with the fuel combustion that burning feedway 21a is supplied with, supplies with combustion flame to refuse A.
Be provided with the sprinkler pipe 22 that passes its upper portion side wall at vapourizing furnace 1.Sprinkler pipe 22 is connected by the water source by the open and close valve 23 of control device 18 trip switchs and not shown aqua storage tank etc., and the while can spill the water of supplying with from described water source in vapourizing furnace 1 at its front end band Water spray nozzle 24.
Roasting kiln 3 is by mixing by the inflammable gas that destructive distillation produced of refuse A and making the burning portion 25 of the needed oxygen of its perfect combustion (air) and the inflammable gas incendiary combustion chamber 26 with oxygen mix is constituted, and combustion chamber 26 is connected with this burning portion 25 at the front end of burning portion 25.Connect gas passage 2 in the rear end of burning portion 25, the inflammable gas that destructive distillation produced by the refuse A in vapourizing furnace 1 imports to burning portion 25 through gas passage 2.
In the empty chamber 27 that the peripheral part of burning portion 25 has and it is inner isolated, this sky chamber 27 is by in a plurality of nozzle bores that interior perimembranous wore 28 of burning portion 25 and the internal communication of burning portion 25.Be connected to sky chamber 27 from the roasting kiln of 14 shunt of main oxygen feedway with oxygen feedway 29.At the roasting kiln control valve 31 that is provided with on the oxygen feedway 29 by valve actuator 30 its switchings of control, valve actuator 30 is by described control device 18 controls.
Rearward end in burning portion 25 is installed the combustion unit of being controlled by control device 18 32, in this combustion unit, makes the combustion-supporting oil firing of the heavy oil supplied with fuel feed road 21b by main fuel feedway 21, roasting kiln from burning feedway 20 etc.Combustion unit 32 is made of pilot burner etc., and described combustion-supporting oil is burnt with described inflammable gas.In addition, combustion unit 32 also is used to light the inflammable gas that imports to burning portion 25.
The ventilation duct 33a of the waste gas of discharge after the 26 inflammable gas perfect combustions of combustion chamber is set at the front end of combustion chamber 26.Ventilation duct 33a is shunted to ventilation duct 33a in pipeline 1, 33a 2Two, ventilation duct 33a 1Be connected to an end of the 1st heat exchanger 34, and ventilation duct 32a 2Be connected to ash handling plant 4 as described later.The inside of the 1st heat exchanger 34 is provided with main oxygen feedway 14, heats described oxygen by carrying out heat exchange at described waste gas and this between the oxygen of main oxygen feedway 14.
At the ventilation duct 33b that connects the waste gas after discharge is carried out heat exchange with described oxygen on the other end of the 1st heat exchanger 34 1Ventilation duct 33b 1The dirty of the 1st heat exchanger 34 with from the ventilation duct 33b of 4 combustion gas of described ash handling plant 2The interflow becomes ventilation duct 33b, by gas blower 35 described waste gas is discharged to the atmosphere from chimney 36.In addition, cyclone scrubber 37, cooling tower 38, deep bed filter 39 are set in the pipeline of ventilation duct 33b.
In addition, in the device of present embodiment, in gas passage 2, connect to divide and get the branch that imports to a part of inflammable gas of roasting kiln 3 from vapourizing furnace and get conduit 40, being divided the inflammable gas of getting to import oil content retrieving arrangement 42 by check valve 41.Oil content retrieving arrangement 42 is by condenser 43a, the 43b of the condensing inflammable gas of being got by branch and further be recovered in condenser 43a, 43b and do not disembarked by the oil content of condensing combustible component and 44 constitute.Oil content is disembarked and 44 is connected to roasting kiln 3 by gas duct 45, contain at oil content 44 gases that do not have an isolating combustible component of disembarking and import to the combustion chamber 26 of roasting kiln 3 through gas blower 46, make with the inflammable gas that imports to roasting kiln 3 from gas passage 2 and burn by gas duct 45.
The storage tanks 47a, the 47b that store respectively by condensing oil content are set below condenser 43a, 43b.Derived from oil storage vessel 47a, 47b by refiltered oil conduit 48 by condensing oil content at condenser 43a, 43b, behind oil-water separator 49, strainer 50, be sent to fuel supply system 20 by pump 51.In addition, the main fuel feedway 21 of deriving fuel from fuel supply system 20 is shunted to three branch roads halfway, promptly described vapourizing furnace with fuel feed road 21a and roasting kiln with fuel feed road 21b and the melting furnace usefulness fuel feed road 21c that is connected to ash handling plant 4 described later.
And, in the device of present embodiment, the temperature T in the top of vapourizing furnace 1 installation and measuring vapourizing furnace 1 1Temperature sensor 52, on roasting kiln 3, detect the temperature T in the roasting kiln 3 2Temperature sensor 53 be installed to the leading section of contiguous burning portion 25.The detection signal of temperature sensor 52,53 is imported into control device 18.
Ash handling plant 4, as shown in Figure 2, have worm conveyor 54 set below the ash outlet 8 of in vapourizing furnace 1, discharging calcination B, along the set above it flux adding set 55 of worm conveyor 54, pack into and the melting furnace 56 of the mixture C of the calcination B flux that fusion is carried by worm conveyor 54, be dropped in the melts D of melting furnace 56 gained and make it the tank 57 of chilling, the travelling belt 58 of output slag E from tank 57.Melting furnace 56 is by the mixture C of pack into described calcination B and flux and heat with fused melter 59, constitute with the flue 61 that the bottom of putting into the chute portion 60 of tank 57 at the melts D of melter's 59 gained and being located at melter 59 is connected with chute portion 60 before the leading section of melter 59 is communicated with and discharge the waste gas of melting furnace 56.
Be provided with the input port 63 that freely openable drops into door 62 facial having in melter 59, and can be from the input port 63 the calcination B that is carried by worm conveyor 54 and the mixture C of flux be put in the melter 59.In addition, connect from the ventilation duct 33a of ventilation duct 33a shown in Figure 1 institute shunt in melter 59 2, make a part of waste gas that imports roasting kiln 3.
Become the inclined-plane at the top of chute portion 60 60a, on the 60a of this top, install as the mixture C in burner 64, the 64 sensing melter 59 of heating unit.Burner 64,64 is by making the mixture C in the fuel combustion heating and melting chamber 59 that fuel supply system shown in Figure 1 20 is supplied with fuel feed road 21c by main fuel feedway 21, melting furnace.
In addition, supplying with the melting furnace that burns with oxygen is connected with burner 64 with oxygen feedway 65.Melting furnace is collaborated to constitute by air feedway 65a that connects the air supply source 66 that is made of gas blower etc. and the purity oxygen feedway 65b that is connected the pure oxygen source of the gas 67 that is made of oxygen cylinder etc. with oxygen feedway 65, the air supplied burner 64 that contains the oxygen of the high density of mixing purity oxygen in air.
The ventilation duct 33b of the waste gas behind the mixture on the front of flue 61 in connection discharge heating and the fusion melter 59 2, ventilation duct 33b 2Be connected on the ventilation duct 33b shown in Figure 1 by the 2nd heat exchanger 68, tornado dust collector 69.In described the 2nd heat exchanger 68 air feedway 65a is set, by by ventilation duct 33b 2Carry out heat exchange between the air that is circulated among described waste gas of being supplied with and the air feedway 65a, heat described air,
Secondly, the incineration treatment method embodiment 1 of the refuse of the present invention of using said apparatus is described with reference to Fig. 1-Fig. 3.
In device shown in Figure 1, during burning disposal refuse A, at first open and drop into door 5, from input port 6 refuse A is put in the vapourizing furnace 1.Mixing is based on the various refuses of damaged tire and adjust described refuse A and make when stable by the combustion gas that destructive distillation was produced in the vapourizing furnace 1 and to have its temperature of combustion when burning away be heat more than 850 ℃.
Then, close drop into door 5 make become air-tight state in the vapourizing furnace 1 after, before lighting described refuse A, make combustion unit 32 work of roasting kiln 3 by control device 18, begin the burning of combustion-supporting oil.When by the temperature T in the temperature sensor 53 detected roasting kilns 3 2When surpassing 800 ℃ of the possible pyrolysated of dioxin, started the portfire 19 of vapourizing furnace 1 by control device 18 and light refuse A, part refuse A takes fire.
A takes fire when the part refuse, by temperature sensor 52 detected temperature T 1Reach the temperature T of regulation 1AThe time, then stop portfire 19 by control device 18.When the underclad portion of refuse A takes fire, then make the top section destructive distillation of this refuse A by its combustion heat, import to the burning portion 25 of roasting kiln 3 by the gas passage 2 that is connected with this vapourizing furnace 1 by the inflammable gas that destructive distillation produced.
Import to the inflammable gas of burning portion 25, in burning portion 25, light, in combustion chamber 26, take fire with described combustion-supporting oil with the oxygen mix of being supplied with oxygen feedway 29 from roasting kiln and by the combustion flame of being supplied with from combustion unit 32.When the burning of described inflammable gas begins, because the generation instability of described pyrogenous inflammable gas, this inflammable gas can not stable supplying roasting kiln 3, but stable and produce described inflammable gas continuously along with the destructive distillation vapourizing furnace 1 in, its generation is constantly increase also.
Along with the increase of the generation of described inflammable gas, the temperature T in roasting kiln 3 2During rising, described inflammable gas can spontaneously be stablized and be burnt away by the combustion heat of self.In addition, if the temperature T in the roasting kiln 3 that is detected by temperature sensor 53 2, for example become more than 830 ℃, then control device 18 stops the burning by the combustion-supporting oil of combustion unit 32, by the temperature T after stopping 2Variation, judge that can inflammable gas spontaneously stablize and burn away.
Its result is by the burning of the combustion-supporting oil of combustion unit 32, the temperature T in roasting kiln 3 2Be then to stop more than 830 ℃, and begin again with next, carry out discontinuously when becoming 830 ℃.Temperature T during this in roasting kiln 3 2, as shown in Figure 3, zig-zag ground changes.Then, if even stop the burning of combustion-supporting oil, the temperature T in the roasting kiln 3 2Also can remain on more than 830 ℃, then control device 18 judges that described inflammable gas reaches spontaneously incendiary state by the combustion heat energy of oneself, stops the burning of combustion-supporting oil., only carry out inflammable gas spontaneous burning, the temperature T in the roasting kiln 3 that is detected with temperature sensor 53 thereafter 2In fact the temperature of combustion that shows this inflammable gas self.
When only carrying out the spontaneous combustion of inflammable gas, by the temperature T in the roasting kiln 3 2Self temperature of combustion of the inflammable gas that is detected can remain on the temperature more than 830 ℃, for example 850 ℃ of substantially constants.At this moment, control device 18 is automatically controlled roasting kiln and is made to supply with to burning portion 25 with the degree of opening of the control valve 31 of oxygen feedway 29 and be the abundant oxygen of measuring of this inflammable gas perfect combustion institute necessity.In addition, the while is according to the temperature of combustion T of the inflammable gas in the roasting kiln 3 that is detected with temperature sensor 53 2, control device 18 is adjusted at the generation of the described inflammable gas in the vapourizing furnace 1 by the degree of opening of automatically controlling control valve 17, and makes the temperature of combustion T of the inflammable gas in roasting kiln 3 2Remain on 850 ℃ substantially constant.
In addition, the temperature T in the vapourizing furnace 1 that is detected by temperature sensor 52 1, in the running of described combustion unit 32, along with the burning of the lower layer part of refuse A after lighting described refuse A enlarges and rises, but thereafter the combustion heat of the lower layer part of refuse A because the destructive distillation of upper layer part is consumed temporary transient decline.Then, cease combustion device 32 only carries out the spontaneous burning of described inflammable gas, when entering the stage (temperature T in the roasting kiln 3 that described destructive distillation is stably carried out in accordance with regulations 2Remain on the stage of 850 ℃ of substantially constants), the temperature T in the vapourizing furnace 1 then 1Turn to rising once more, and then rise along with carrying out described destructive distillation.
Only carrying out the spontaneous combustion phases of described inflammable gas, the generation of inflammable gas is vigorous, even divide a part of getting this inflammable gas, the temperature T in substantially constant ground keeps roasting kiln 3 2Be still can obtain sufficient inflammable gas under 850 ℃.Therefore, get the part that conduit was got described inflammable gas in 40 minutes by branch, and reclaim as oil content at the contained combustible component of this inflammable gas by 42 of oil content retrieving arrangements in this stage.
When the pressure of the inflammable gas in the gas passage 2 surpasses specified pressure, import at the check valve through too getting conduit 40 41 in the inflammable gas of oil content retrieving arrangement 42, the combustible component of liquefaction by condensing, carries out the recovery of described oil content at condenser 43a, the 43b of configured in series at first easily.After the oil content that is liquefied is encased in storage tanks 47a, 47b, be removed by pump 51.Described oil content is delivered to burning feedway 20, and is respectively supplied with the portfire 19 of vapourizing furnace 1, the combustion unit 32 of roasting kiln 3, the burner 64 of melting furnace 56 with fuel feed road 21b, roasting kiln with fuel feed road 21c with fuel feed road 21a, roasting kiln by vapourizing furnace from main fuel feedway 21 at oil-water separator 49, strainer 50 after refining.
Then, be not sent to oil content at condenser 43a, 43b and disembark 44, and combustible component is recovered as oil content by condensing described inflammable gas.And be directed to the combustion chamber 26 of roasting kiln 3 and make it perfect combustion by gas blower 46 by gas duct 45 at the disembark inflammable gas of 44 remnants that are not recovered of oil content.
In roasting kiln 3, the waste gas after the inflammable gas perfect combustion at first is discharged to ventilation duct 33a, and a part of waste gas is by ventilation duct 33a 1Be sent to the 1st heat exchanger 34, be used to heat the oxygen that is circulated in the main oxygen feedway 14 that in the 1st heat exchanger 34, is set.In addition, be discharged to all the other waste gas of ventilation duct 33a by ventilation duct 33a 2Be sent to the melter 59 of melting furnace 56.Acting on the back and will be described for the waste gas that imports to melter 59.
Be used to heat the waste gas of described oxygen from ventilation duct 33b at the 1st heat exchanger 34 1By, ventilation duct 33b is directed to cyclone scrubber 37, and removes dust contained in this waste gas.Then, described waste gas is cooled fully by being directed to cooling tower 38, is imported into deep bed filter 39 afterwards.Then, in deep bed filter 39, further be removed fine flying dust, be discharged into the atmosphere from chimney 36 by gas blower 35 at last.
Then, when the energy destructive distillation of the destructive distillation of the refuse A in carrying out vapourizing furnace 1 and refuse A partly tails off, then adjusting the degree of opening of vapourizing furnace with the control valve 17 of oxygen feedway 13, even and increase oxygen feed rate to vapourizing furnace 1, can not be produced as the interior temperature T of roasting kiln 3 2Remain on the inflammable gas of 850 ℃ abundant amount, the temperature T in the roasting kiln 3 substantially constant 2Show and have from the tendency of 850 ℃ of reductions.
In addition, if the temperature T in the roasting kiln 3 2, for example be that control device 18 begins the burning by the combustion-supporting oil in the combustion unit 32 again below 830 ℃.In this stage, if the temperature T in the roasting kiln 3 2Be more than 830 ℃, control device 18 stops the burning by the combustion-supporting oil of combustion unit 32, by the temperature T of the roasting kiln after stopping 3 2Variation, judge whether inflammable gas can spontaneously be stablized and be burnt away.
Its result is by the burning of the combustion-supporting oil of combustion unit 32, the temperature T in roasting kiln 3 2Stop once becoming more than 830 ℃, and be just to begin once more below 830 ℃, carry out intermittently, at this moment, the temperature T in the roasting kiln 3 2, as shown in Figure 3, change zigzag.Then, when the burning of the combustion-supporting oil that does not carry out oil combustion device 32, if the temperature T in the roasting kiln 3 2Can not arrive more than 830 ℃, then control device 18 is judged fully spontaneously incendiary state of described inflammable gas, as mentioned above, proceeds the burning of combustion-supporting oil, makes the temperature T in the roasting kiln 3 2Remain on more than 800 ℃.
On the other hand, when the part of the pyrogenous refuse A of energy tails off, because refuse A directly burns in vapourizing furnace 1, so the temperature T in the vapourizing furnace 1 1Rise hastily.Then, the pyrogenous part of the energy of refuse A is used up, and the refuse A of red heatization becomes ashing, temperature T at this moment 1MAXAs top temperature, and turn to minimizing.But, the each processing because the capacity of refuse A, material etc. are various, thus below the upper layer of ashing the remaining part that red heatization is arranged or also do not have red heatization, owing to this part might make vapourizing furnace T 1Interior temperature raises once more.
In addition, when the burning do not carried out by the combustion-supporting oil of combustion unit 32, the temperature T in roasting kiln 3 2Can not be raised to the stage more than 830 ℃, control device 18 is in per specified time, and for example per 10 minutes the temperature T in the vapourizing furnace 1 that is detected by temperature sensor 52 1With the top temperature T in the vapourizing furnace 1 1MAXRelatively.Then, the temperature in vapourizing furnace 1 is at continuous stipulated number, and for example 3 times less than top temperature T 1MAXThe time, control device 18 judges that the refuse A in the vapourizing furnace 1 is transformed into ashing reliably fully.Afterwards, the temperature T in the vapourizing furnace 1 1Ashing with refuse A decreases.
In the past, discharging the operation of the burning residue (calcination B) of refuse A from vapourizing furnace 1, is the temperature T of waiting in the vapourizing furnace 1 1Be reduced to the temperature of easy processing calcination B, for example the normal temperature degree is carried out.But, because waiting temperature T 1Be reduced to the normal temperature degree, so reduce under the temperature and need can not put into vapourizing furnace to new refuse in this period, so the processing cycle is elongated for a long time.
In addition, in the present embodiment, can destructive distillation in vapourizing furnace 1 part of refuse A tail off, judge that by control device 18 refuse A in the vapourizing furnaces 1 all is converted to ashing reliably after, the temperature in the vapourizing furnace 1 is from top temperature T 1MAXBegin to reduce, in the time of become less than the generation temperature of dioxin 250-350 ℃, for example be below 200 ℃, shown in the dotted line of Fig. 2, open base plate 10a, the 10b of the ash output hole 9 of vapourizing furnace 1 immediately, discharge by vapourizing furnace 1 interior calcination B is fallen downwards.
In the present embodiment, if discharge calcination B in the vapourizing furnace 1 fully, then close base plate 10a, 10b, open simultaneously and drop into door 5,6 put into new refuse A in the vapourizing furnace 1 again from the input port.At this moment, as previously mentioned, the temperature in the roasting kiln 3 is maintained at more than 800 ℃, so can directly light the refuse A that is encased in once more in the described vapourizing furnace 1, then, carries out following burning disposal by said process.
Like this, owing to the temperature T that does not wait in the described vapourizing furnace 1 1Reduce, discharge the calcination B in the vapourizing furnace 1 and can reinstall in the vapourizing furnace 1, so can shorten the processing cycle to new refuse A, in addition, when a new refuse A is reinstalled, utilize the processing of last time to have surplus heat in the vapourizing furnace 1 and heat, so after the igniting, can make the easy stabilization of partial combustion of refuse A.
Below, the processing of handling the calcination B that is discharged from vapourizing furnace 1 is described.When discharging described calcination B, the temperature in the vapourizing furnace 1 as previously mentioned, is reduced to 200 ℃ less than the generation temperature of dioxin, so needn't worry to produce dioxin from described calcination B.But, because described calcination B still is a high temperature, so it is promptly imported to melting furnace 56 and fusion.
At present embodiment,, as shown in Figure 2, on the spiral conveyer 54 of the below of the ash outlet 9 that calcination B is fallen be arranged on vapourizing furnace 1, and carry by spiral conveyer 54 for described calcination B is promptly imported to melting furnace 56.When discharging described calcination B, before opening base plate 10a, 10b, open open and close valve 23 on the sprinkler pipe 22 in required time by control device 18 as shown in Figure 1, upper strata watering from the calcination B of Water spray nozzle 24 in vapourizing furnace 1, like this, when falling spiral conveyer 54, described calcination B can prevent that calcination B from dispersing.After taking out described calcination B from vapourizing furnace 1 as mentioned above, in melting furnace 56 heating and fusions, described watering can make the upper layer part of calcination B be integral by water and get final product, and need not sprinkle water too much.In addition, after open and close valve 23 is opened the specified time, close by control device 18 again.
Then, open the input door 62 of melting furnace 56,63 calcination B put into melting furnace 56 from the input port by spiral conveyer 54.Flux adding set 55 is set above spiral conveyer 54.In the present embodiment, add to the calcination B that is passed on by spiral conveyer 54 from solvent adding set 55 as the silica sand of flux and the mixture of Wingdale.Because silica sand and Wingdale are all cheap, to favourable on the control operating cost.Described calcination B mixes with silica sand and Wingdale in carrying on the way by spiral conveyer 54, and the mixture C of calcination B and silica sand and Wingdale is put in the melter 59 of melting furnace 56.
In melter 59, by from ventilation duct 33a ventilation duct 33a along separate routes 2Import the waste gas of roasting kiln 3, this waste gas has the temperature more than 850 ℃.In addition, before dropping into mixture C, start burner 64.
In addition, described mixture is by waste gas heating, and directly heated by the combustion flame of burner 64.Described mixture C as mentioned above, contain calcination B this as high temperature since with silica sand and Wingdale mixed melting point step-down as flux, therefore by heating easy fusion and becoming melts D.
When described fusion, though contained in calcination B, not clean-burning refuse A is by perfect combustion, but as previously mentioned,, needn't worry to produce dioxin by the burning of refuse A owing in melter 59, imported the waste gas of the temperature more than 850 ℃ of roasting kiln 3.
As mentioned above, the melts D that is melted flow to the leading section of melter 59, automatically falls in the chute 60, and puts in the tank set below chute portion 60 57.Put into the water of melts D by institute's contain in tank 57 in the tank 57 and carry out chilling and be broken, form tiny granulous solid substance (slag E).
Described slag E is discharged from from tank 57 by the conveying belt 58 that is arranged in the tank 57.In addition, described silica sand is mixed to the fusing point that reduces mixture C among the calcination B, is melt into simultaneously to be the glassiness, so contained objectionable impuritiess such as weight metal can be encased in the described slag E in calcination B, can prevent that it from spilling.
The waste gas of described melting furnace 56 from melter 59 through slide groove portion 60, flue 61 and by ventilation duct 32b 2Be discharged from.This waste gas is at ventilation duct 33b 2In the air that circulated with air feedway 65a set this heat exchanger 68 in set the 2nd heat exchanger 68 carry out heat exchange, and collaborate to be discharged in the atmosphere by chimney 36 with ventilation duct 33b shown in Figure 1 after removing dust by cyclone scrubber 69 with the waste gas of roasting kiln 3.
The burner 64 of described melting furnace 56 makes by by the main fuel feedway 21 of fuel supply system 20, the fuel that melting furnace is supplied with fuel feed road 21c, utilizes the combustion air of being supplied with oxygen feedway 65 by melting furnace to burn.Described combustion air is by carrying out mixing in the heated air of heat exchange the purity oxygen of being supplied with through purity oxygen feedway 65b by from purity oxygen supply source 67 with the described waste gas of being supplied with by air feedway 65a.Its result has improved the oxygen concentration of described combustion air, makes burner 64 can obtain the high temperature firepower that is more suitable for for molten mixture C.
Secondly, the incineration treatment method of the 2nd kind of refuse of present embodiment is described with reference to Fig. 4.
At the destructive gasifying incinerating and treating device of the used refuse of present embodiment, except that the structure of ash handling plant 4, have the device identical structure used with the foregoing description 1.Ash handling plant 4 at present embodiment, as shown in Figure 4, remove roasting and melt the ash outlet 9 that the input port 63 of stove 56 is connected to vapourizing furnace 1, base plate 10a, 10b are driveed in input port 63, make beyond flux directly puts in the input port 63 from flux adding set 55, and be entirely same structure at embodiment 1 ash handling plant 4 used, as shown in Figure 2.
Below, the embodiment 2 with the incineration treatment method of the refuse of this device is described.In the present embodiment, the situation of the burning of refuse and the foregoing description 1 is fully similarly carried out.Part that can pyrogenous refuse A in vapourizing furnace 1 tails off, and after judging that by control device 18 refuse A in the vapourizing furnaces 1 becomes ashing really fully, the temperature T in vapourizing furnace 1 1From top temperature T 1MAXDuring decline, shown in Fig. 4 dotted line, open base plate 10a, the 10b of ash outlet 9, make the calcination B in the vapourizing furnace 1 fall and be discharged from downwards.
Then, in the present embodiment, except that flux is directly put in the input port 63 from flux adding set 55, by fully similarly handling with the situation of described embodiment 1, fusion calcination B, and form slag E by melts D.In the present embodiment, because calcination B is the temperature T in vapourizing furnace 1 1Being discharged from before being reduced to the generation temperature less than dioxin, is sufficient high temperature therefore, can carry out fusion easily.
In the used ash handling plant 4 of present embodiment, the input port 63 of melting furnace 56 shown in Figure 4 is configured to be connected with the ash outlet 9 of vapourizing furnace 1, so one opens base plate 10a, 10b, then calcination B does not contact the melter 59 that is put to melting furnace 56 with outer border air.Therefore, at present embodiment, do not wait until the temperature T in the vapourizing furnace 1 1Be reduced to the temperature that can not generate dioxin, for example in described temperature T 1When being 300 ℃, discharge calcination B, and can carry out the input again of new refuse A, can further shorten the processing cycle.

Claims (12)

1. the incineration treatment method of a refuse has and lights the part burning that the refuse that is encased in the vapourizing furnace makes this refuse, by the operation of its all the other refuses of combustion heat destructive distillation with imported to the roasting kiln operation that makes it to burn by the inflammable gas that destructive distillation produced;
When in this roasting kiln, burning inflammable gas, amount according to the inflammable gas that imports to this roasting kiln is supplied with its this inflammable gas of needed oxygen combustion that burns to this roasting kiln, simultaneously, make temperature variation in this roasting kiln according to burning by this inflammable gas in this roasting kiln, the amount of oxygen that control is supplied with to this vapourizing furnace is also adjusted amount by the inflammable gas that destructive distillation produced, and the temperature in this roasting kiln is remained on basic constant temperature more than the specified temperature; It is characterized in that, also comprise:
Along with the refuse in the described vapourizing furnace carries out destructive distillation, can reduce by pyrogenous waste part in this vapourizing furnace, temperature in this roasting kiln reduces from top temperature, not arriving when generating the temperature of dioxin by this refuse, directly takes out the operation that this burns remnant from this vapourizing furnace; With
After taking out this burning residue from this vapourizing furnace, the operation of in this vapourizing furnace, packing new refuse into and lighting.
2. the incineration treatment method of refuse according to claim 1, it is characterized in that pack into melting furnace and carry out heating and melting of the burning residue of getting from described vapourizing furnace, carry out chilling in the water and become granular solid substance by melts is dropped into then by heating unit set on this melting furnace.
3. the incineration treatment method of refuse according to claim 2 is characterized in that adding solvent in described burning residue.
4. according to the incineration treatment method of claim 2 or 3 described refuses, when it is characterized in that dissolving burning residue, in described roasting kiln, make by the inflammable gas that destructive distillation the produced burning of the refuse in vapourizing furnace and the waste gas that is produced and import to described melting furnace, and heat described burning residue.
5. according to the incineration treatment method of claim 2,3 or 4 described refuses, the heating unit that it is characterized in that being arranged on described melting furnace is a combustion unit, and supplying with this combustion unit by the oxygen that heat heated of described melting furnace.
6. the incineration treatment method of refuse according to claim 5, it is characterized in that when the inflammable gas that destructive distillation produced by the refuse in the described vapourizing furnace being imported to described roasting kiln when making it to burn, divide and get this inflammable gas of a part, make it condensing and the recovery oil content, simultaneously, this profit is arranged on the fuel of the combustion unit in the described melting furnace.
7. according to the incineration treatment method of each described refuse among the claim 1-6, it is characterized in that from this vapourizing furnace, taking out this burning residue after the upper strata watering of the burning residue in described vapourizing furnace.
8. the incineration treatment method of a refuse has and lights the refuse that is encased in the vapourizing furnace and make this trash burning of a part and make it the incendiary operation by the operation of its all the other refuses of combustion heat destructive distillation with importing to roasting kiln by the inflammable gas that this destructive distillation produced;
When this roasting kiln burns this inflammable gas, amount according to the inflammable gas that imports to this roasting kiln is supplied with its this inflammable gas of needed oxygen combustion that burns to this roasting kiln, simultaneously, according to by making temperature variation in this roasting kiln by the burning of this inflammable gas in this roasting kiln, the amount of oxygen that control is supplied with to this vapourizing furnace is also adjusted amount by the inflammable gas that this destructive distillation produced, and the temperature in this roasting kiln is remained on basic constant temperature more than the 1st specified temperature; It is characterized in that, also comprise:
Along with the refuse in the described vapourizing furnace carries out destructive distillation, can reduce by pyrogenous waste part in this vapourizing furnace, temperature in this roasting kiln becomes less than behind the described basic constant temperature, when the temperature in this vapourizing furnace when top temperature reduces, from this vapourizing furnace, take out this burning residue, and be encased in the operation of the melting furnace that is connected with on this vapourizing furnace by the burning residue conveying end;
Heat and this burning residue of fusion by the heating unit that is arranged on this melting furnace, and carry out the operation that chilling becomes granular solid substance by melts is dropped in the water; With
After taking out this burning residue from this vapourizing furnace, the operation of packing new refuse into and lighting at this vapourizing furnace.
9. the incineration treatment method of refuse according to claim 8 is characterized in that adding solvent and make its fusion in described burning residue.
10. according to Claim 8 or the incineration treatment method of 9 described refuses, when it is characterized in that when dissolving burning residue, the waste gas that the inflammable gas that destructive distillation the produced burning that makes in described roasting kiln by the refuse in vapourizing furnace is produced imports to described melting furnace, and heats described burning residue.
11. according to Claim 8, the incineration treatment method of 9 or 10 described refuses, the heating unit that it is characterized in that being arranged on described melting furnace is a combustion unit, and supplying with this combustion unit by the oxygen that heat heated of described melting furnace.
12. the incineration treatment method of refuse according to claim 11, it is characterized in that when the inflammable gas that destructive distillation produced by the refuse in the described vapourizing furnace being imported to described roasting kiln when making it to burn, branch is got this inflammable gas of a part to be made it condensing and the recovery oil content, simultaneously this oil content is made the fuel of the combustion unit that is arranged on described melting furnace.
CNB998104558A 1998-09-22 1999-09-14 Waste incineration disposal method Expired - Fee Related CN1213128C (en)

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JP26865698 1998-09-22
JP268656/1998 1998-09-22

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CN104946312A (en) * 2015-06-30 2015-09-30 大连理工大学 Novel gasifying-incinerating coupled melting method for co-producing fuel gas and inorganic materials
CN106765146A (en) * 2016-12-30 2017-05-31 重庆科技学院 Secondary pollutant control system based on waste gasification melt-combustion
CN111828988A (en) * 2019-04-23 2020-10-27 B&G韩国株式会社 Mixed combustion processing device for organic residual waste resources
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CN103353116A (en) * 2013-07-01 2013-10-16 广东博海昕能环保有限公司 Automatic combustion control system
CN103557529A (en) * 2013-11-15 2014-02-05 宜兴市智博环境设备有限公司 Pyrolyzed waste gas burning heat energy circulation and flue gas purification system
CN103557529B (en) * 2013-11-15 2016-03-16 宜兴市智博环境设备有限公司 Cracking burned waste gas heat circulation and flue gas purification system
CN104946312A (en) * 2015-06-30 2015-09-30 大连理工大学 Novel gasifying-incinerating coupled melting method for co-producing fuel gas and inorganic materials
CN106765146A (en) * 2016-12-30 2017-05-31 重庆科技学院 Secondary pollutant control system based on waste gasification melt-combustion
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CN117304953A (en) * 2022-03-25 2023-12-29 北京丰润铭科贸有限责任公司 Combustible wood base, paper base and other combustible waste treatment systems

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CN1213128C (en) 2005-08-03
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WO2000017289A1 (en) 2000-03-30

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