CN115031236A - Organic hazardous waste integrated plasma multi-stage gasification melting furnace device, system and method - Google Patents

Organic hazardous waste integrated plasma multi-stage gasification melting furnace device, system and method Download PDF

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CN115031236A
CN115031236A CN202210629984.4A CN202210629984A CN115031236A CN 115031236 A CN115031236 A CN 115031236A CN 202210629984 A CN202210629984 A CN 202210629984A CN 115031236 A CN115031236 A CN 115031236A
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flue gas
gasification
furnace
temperature
plasma
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蒋太波
章鹏兴
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Chengdu Huanfu Technology Co ltd
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Chengdu Huanfu Technology Co ltd
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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
    • F23G5/006—General arrangement of incineration plant, e.g. flow sheets
    • 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
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/04—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment drying
    • 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
    • F23G5/085—High-temperature heating means, e.g. plasma, for partly melting the waste
    • 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
    • F23G5/10—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating electric
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/14—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
    • F23G5/16—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion in a separate combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/20—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having rotating or oscillating drums
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F23G5/46—Recuperation of heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/006—Layout of treatment plant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/10—Drying by heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/40—Gasification
    • 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
    • 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
    • F23G2204/00—Supplementary heating arrangements
    • F23G2204/10—Supplementary heating arrangements using auxiliary fuel
    • F23G2204/103—Supplementary heating arrangements using auxiliary fuel gaseous or liquid fuel
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    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2204/00—Supplementary heating arrangements
    • F23G2204/20—Supplementary heating arrangements using electric energy
    • F23G2204/201—Plasma
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/20—Waste heat recuperation using the heat in association with another installation
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    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/10—Nitrogen; Compounds thereof
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    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/20—Sulfur; Compounds thereof
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    • 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
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    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/30—Halogen; Compounds thereof
    • F23J2215/301—Dioxins; Furans
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    • F23J2215/00—Preventing emissions
    • F23J2215/60—Heavy metals; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2217/00—Intercepting solids
    • F23J2217/10—Intercepting solids by filters
    • F23J2217/101—Baghouse type
    • 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
    • F23J2217/10—Intercepting solids by filters
    • F23J2217/102—Intercepting solids by filters electrostatic
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/10—Catalytic reduction devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/30—Sorption devices using carbon, e.g. coke

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Plasma & Fusion (AREA)
  • Gasification And Melting Of Waste (AREA)

Abstract

The invention discloses an integrated multistage plasma gasification melting furnace device, system and method for organic hazardous wastes. The invention adopts two-stage gasification treatment, reduces the operation load of the plasma torch and improves the reliability of the gasification melting process, thereby reducing the installation and operation power of the plasma torch, obviously enhancing the material universality and economy of the integrated plasma gasification melting treatment of the organic hazardous wastes, and reducing the investment operation cost of the industrial application of the plasma gasification melting of the organic hazardous wastes.

Description

Organic hazardous waste integrated plasma multi-stage gasification melting furnace device, system and method
Technical Field
The invention relates to the field of organic hazardous waste treatment technology and equipment, in particular to an organic hazardous waste integrated plasma multi-stage gasification melting furnace device, system and method, and belongs to the technical field of organic hazardous waste treatment.
Background
The comprehensive treatment of organic hazardous wastes mainly adopts rotary kiln incineration technology. When a rotary kiln is used for comprehensively incinerating and treating various kinds of organic hazardous wastes, the problems of incomplete reaction, high burning rate of incineration residues, small actual treatment capacity, dioxin pollution and the like exist, the incineration residues and fly ash still belong to hazardous wastes, further stabilization, solidification and landfill treatment are needed, the pollution hidden danger of soil and underground water can be formed, and the large-scale, clean and resource development of a rotary kiln incineration technology is hindered.
When various types of organic hazardous wastes are treated by pyrolysis and gasification through a fixed bed, the fixed bed is limited by the thermochemical reaction kinetics of the organic hazardous wastes, the pyrolysis and gasification process is slow, the temperature is low, the pyrolysis and gasification are not thorough, a large amount of solid semicoke with high carbon content can be generated, the thermal ignition rate of the pyrolysis and gasification semicoke is far higher than 5%, and the requirement of hazardous waste incineration pollution control standard cannot be met; meanwhile, the pyrolysis gasification reaction conditions of the multi-component organic matters are different, and the organic matters generate a large amount of tar by random chain scission, so that pyrolysis gasification equipment and a flue are blocked, and the system has poor material universality and poor operation reliability.
The rotary anaerobic pyrolysis treatment of organic hazardous wastes adopts an indirect heating mode, the heat of an outer jacket heats the organic matters through a rotary kiln cylinder in a heat conduction and heat radiation mode, the rotary anaerobic pyrolysis furnace has low heat transfer efficiency, and the equipment is difficult to amplify; the pyrolysis temperature in the furnace is low due to the limitation of the thermal stress of the rotary kiln and the temperature resistance of furnace body materials; the pyrolysis reaction conditions of the organic matters are different, the organic matters are randomly broken, the components of the pyrolysis product are dispersed, the product quality is low, the directional regulation and control of the product are difficult, and the resource degree is low; the rotary anaerobic pyrolysis has poor material adaptability and is only suitable for treating specific and single-kind organic hazardous wastes.
At present, when a rotary kiln incineration technology and a fixed bed pyrolysis gasification technology are used for comprehensively treating various kinds of organic hazardous wastes, the effective control and adjustment of a thermochemical reaction process are lacked, and the method mainly comprises the stages of material drying, pyrolysis, gasification, combustion and the like. The drying process is influenced by the water content of the materials, and different drying sections can be presented in the furnace; the organic matters can be heated and decomposed in the high-temperature environment in the furnace, and different pyrolysis sections can be presented in the furnace under the influence of the boiling point, the length and the structure of a molecular chain, the pyrolysis temperature and the pyrolysis speed of the organic matters and the operation temperature of the furnace; the organic matter pyrolysis can generate pyrolysis gas-phase products with different components and also can generate pyrolysis solid-phase products taking a pyrolysis semicoke form as a main part, and the carbon content of the pyrolysis semicoke of different types of organic hazardous wastes is different; the gasification and combustion of the pyrolysis semicoke are high in temperature, long in time and large in air quantity, and the gasification and combustion process of the pyrolysis semicoke is extremely slow, so that the gasification and combustion process of the pyrolysis semicoke directly determines the residue thermal ignition reduction rate and the treatment efficiency of a rotary kiln incinerator and a fixed bed pyrolysis gasifier. The difference of the pyrolysis gasification combustion characteristics of the organic hazardous wastes has a crucial influence on the process conditions and the operation parameters such as the feeding speed, the air supply amount, the auxiliary fuel amount, the temperature in the furnace, the oxygen concentration (oxygen content) in the furnace, the smoke gas amount and the like, the regulation and control of the reaction process of the rotary kiln incinerator and the fixed bed pyrolysis gasifier are weak, the control effect on the residue thermal ignition loss rate and the source of carbon monoxide and dioxin pollution is poor, and the large-scale, clean recycling and development of the rotary kiln incineration technology and the fixed bed pyrolysis gasification technology are hindered.
At present, a rotary kiln incinerator, a fixed bed pyrolysis gasifier and a rotary anaerobic pyrolysis furnace have certain defects and limitations in the industrial application aspect of comprehensive treatment of organic hazardous wastes. The rotary kiln incineration technology has strong material universality, but has the problems of high residue thermal ignition loss rate, low treatment efficiency, small actual treatment amount, dioxin pollution and more secondary hazardous wastes; the fixed bed pyrolysis gasifier has the problems of poor material universality, low treatment temperature, slow treatment process, high residue thermal ignition loss rate and more secondary hazardous wastes; the rotary oxygen-free pyrolysis furnace technology has certain resource property, and pyrolysis products can be used as primary alternative fuel or raw materials, but the problems of poor material universality, low thermal efficiency and difficulty in equipment amplification exist. Therefore, the application balance problem of the comprehensive treatment technology of the organic hazardous wastes in the aspects of material universality, monomer device treatment capacity, process regulation, pollution control, secondary hazardous waste discharge reduction, resource utilization and the like is urgently needed to be solved.
At present, the demonstration application of the domestic plasma method for comprehensively treating the organic hazardous waste mainly comprises a plasma pyrolysis furnace, a fixed bed plasma gasification and melting integrated furnace, a pyrolysis furnace and a plasma melting furnace.
The plasma pyrolysis technology adopts a cylindrical vertical furnace, a plasma torch is positioned at the top of a furnace body, plasma jet flow vertically downwards directly acts on organic matters in the furnace, the organic matters are decomposed under the bombardment of plasma, and inorganic ash is melted at high temperature to form glass-state slag; the reaction mechanism of the plasma pyrolysis technology is not clear, and the reaction process is difficult to control effectively; a small part of plasma participates in the pyrolysis reaction, and a large part of plasma heats pyrolysis gas in a heat radiation mode, so that the plasma has low thermal efficiency, low pyrolysis efficiency and high energy consumption.
The fixed bed plasma gasification and melting integrated furnace is influenced by the pyrolysis characteristics of organic matters with different components, and the pyrolysis process is slow, so the material universality is poor.
The technologies of the pyrolysis furnace and the plasma melting furnace are that the pyrolysis furnace and the plasma melting furnace share a set of flue gas purification system, so that various organic hazardous wastes are comprehensively treated; wherein, the fixed bed pyrolysis furnace, the rotary oxygen-free pyrolysis furnace and the fluidized bed pyrolysis furnace can be used as alternative pyrolysis furnace type technologies; however, the problems of poor material universality, low treatment efficiency, difficult regulation and control of the reaction process, incomplete treatment, secondary pollution and the like of the pyrolysis furnace are not effectively solved, and the energy consumption in the plasma melting process of the pyrolysis semicoke is high, so that the comprehensive treatment of the pyrolysis furnace and the plasma melting furnace cannot realize the purposes of cleanness, reclamation and large-scale production.
Disclosure of Invention
The invention aims to solve the technical problem of providing an integrated plasma multi-stage gasification melting furnace device, system and method for organic hazardous wastes, which adopt a method of staged gasification and segmented control to strengthen the regulation and control of the pyrolysis gasification process, semicoke gasification and ash melting process of various organic hazardous wastes, and have the advantages of strong material universality, high gasification efficiency, low plasma energy consumption, low pollutant emission level and no secondary hazardous wastes, and the integrated plasma gasification melting furnace device is convenient to enlarge.
In order to achieve the purpose, the invention adopts the following technical scheme: an organic hazardous waste integrated plasma multi-stage gasification melting furnace device comprises a counter-current rotary type first-stage gasification furnace, a vertical second-stage gasification furnace, a molten pool, an organic hazardous waste spiral feeding device, a fluxing agent feeding device, a combustor, a plasma torch, a first-stage gasification fan, a second-stage gasification fan, an oxygen measuring instrument and a synthesis gas component analyzer.
Further, the counter-current rotary type primary gasification furnace comprises a horizontal rotary furnace body, refractory materials, a kiln tail cover, a kiln head cover, a synthetic gas outlet pipeline, an emergency chimney, a kiln tail sealing system, a kiln head sealing system and a kiln head sight glass; the included angle between the axis of the horizontal rotary furnace body and the horizontal direction is 2-4 degrees; the refractory material is a refractory brick made of corundum-mullite material; the joint of the horizontal rotary furnace body, the kiln tail cover and the kiln head cover forms a double-sealing system through a kiln tail sealing system and a kiln head sealing system, so that the air leakage of the primary gasification furnace is controlled within 2%; the emergency chimney and the synthesis gas outlet are arranged on the kiln tail cover in a centralized manner; the synthesis gas outlet is arranged at the top of the kiln tail cover and is connected with the inlet of the secondary combustion chamber through a pipeline; the kiln head sight glass is arranged on the kiln head cover panel and is intersected with the axial center line of the horizontal rotary furnace body, so that the gasification reaction process of the organic hazardous waste in the primary gasification furnace can be observed conveniently, and the auxiliary adjustment of the primary gasification process conditions and the operation parameters is facilitated.
Further, the vertical secondary gasification furnace comprises a vertical cylindrical furnace body, refractory materials and a sight glass; the top end of the vertical cylindrical furnace body is connected with the bottom of a kiln head cover of the primary gasification furnace in a flange mode; the refractory material adopts refractory bricks made of chrome corundum; the sight glass is arranged at the lower part of the vertical cylindrical furnace body, so that the plasma high-temperature gasification and inorganic ash fusion processes of the primary gasification solid carbocoal in the secondary gasification furnace can be observed conveniently, and the auxiliary adjustment of secondary gasification and fusion process conditions and operation parameters is facilitated.
Further, the molten bath comprises a flat cylinder, refractory material and a tap hole; the top end of the flat cylinder is connected with the bottom end of the secondary gasification furnace in a flange mode; the refractory material is a refractory brick made of chrome-zirconium corundum and used for preventing molten slag corrosion.
Further, the spiral feeding device for the organic hazardous wastes is connected with a kiln tail cover of the counter-current rotary type primary gasification furnace; the fluxing agent feeding device is connected with a kiln hood of the counter-current rotary type primary gasification furnace; the burner is arranged in the middle of a face plate of a kiln head cover of the counter-flow rotary type primary gasification furnace; the plasma torch is positioned at the bottom of the cylinder body of the vertical secondary gasification furnace; the primary gasification fan is connected with a circular kiln hood of the counter-current rotary primary gasification furnace through an air pipe, primary gasification air tangentially enters the kiln hood, and the air turbulence degree in the primary gasification furnace is improved; the secondary gasification fan is connected with the bottom of the vertical secondary gasification furnace through an annular air pipe; the oxygen measuring instrument is positioned on a horizontal pipeline of a synthetic gas outlet of the countercurrent rotary type primary gasification furnace; the synthesis gas component analyzer is positioned on a horizontal pipeline of a synthesis gas outlet of the counter-current rotary type primary gasification furnace.
Furthermore, a kiln tail cover and a kiln head cover of the counter-current rotary type primary gasification furnace are respectively provided with a first temperature sensor and a second temperature sensor; and a third temperature sensor is arranged at the bottom of the vertical secondary gasification furnace.
Furthermore, a kiln tail cover and a kiln head cover of the counter-current rotary type primary gasification furnace are respectively provided with a first pressure sensor and a second pressure sensor; the vertical secondary gasification furnace is provided with a third pressure sensor.
Furthermore, the primary gasification fan and the secondary gasification fan are controlled by frequency conversion, and the primary gasification air quantity and the secondary gasification air quantity are controlled by distribution and are used for controlling the oxygen content of the organic hazardous waste integrated plasma multistage gasification melting furnace device during operation.
Furthermore, the combustor adopts a split structure, and forms a control loop with the first temperature sensor, so that the flow of auxiliary fuel such as diesel oil or natural gas and the flow of combustion air conveyed by a combustor fan are automatically adjusted, and the combustor is used for controlling the temperature of the device during startup and shutdown and adjusting the temperature of the gasification process in the primary gasification furnace during normal operation.
The utility model provides an organic hazardous waste integral type plasma multistage gasification smelting furnace system which characterized in that: comprises an organic hazardous waste integrated plasma multi-stage gasification melting furnace device, an organic hazardous waste pretreatment system, a secondary combustion chamber, a waste heat recovery device, a flue gas purification device, an induced draft fan, a chimney, a fly ash collection system, a sewage treatment system and the like, wherein a discharge port of the pretreatment system is connected with a feed inlet of an organic hazardous waste spiral feeding device and/or a fluxing agent feeding device of the organic hazardous waste integrated plasma multi-stage gasification melting furnace device, a synthetic gas outlet of the organic hazardous waste integrated plasma multi-stage gasification melting furnace device is connected with a flue gas inlet of the secondary combustion chamber, a flue gas outlet of the secondary combustion chamber is connected with a flue gas inlet of the waste heat recovery device, a flue gas outlet of the waste heat recovery device is connected with a flue gas inlet of the flue gas purification device, a flue gas outlet of the flue gas purification device is connected with a flue gas inlet of the induced draft fan, the smoke outlet of the induced draft fan is connected with the inlet of the chimney, and finally the emission of the waste gas reaching the standard is realized; fly ash generated by the waste heat recovery device and the flue gas purification device is collected, granulated and pretreated, then returned to the vertical secondary gasification furnace by the fluxing agent feeding device for melting treatment, and production wastewater generated by the waste heat recovery device and the flue gas purification device is lifted to a sewage treatment system for treatment by a pump.
Further, the flue gas purification device comprises an SNCR denitration device, a quenching device, a dry deacidification device, an activated carbon injection device, a cloth bag dust removal device, a pre-cooling tower, a two-stage wet deacidification tower, a wet electrostatic dust collector, a GGH flue gas heat exchanger, an SGH flue gas reheater and an SCR denitration device which are arranged at a high-temperature section (850-plus-1100 ℃) of the flue gas of the waste heat recovery device; the flue gas outlet of the quenching device and the material outlet of the activated carbon injection device are connected with the flue gas inlet of the dry deacidification device, the flue gas outlet of the dry deacidification device is connected with the flue gas inlet of the cloth bag dust removal device, the flue gas outlet of the cloth bag dust removal device is connected with the flue gas inlet of the pre-cooling tower, the flue gas outlet of the pre-cooling tower is connected with the flue gas inlet of the primary wet deacidification tower, the flue gas outlet of the primary wet deacidification tower is connected with the flue gas inlet of the secondary wet deacidification tower, the flue gas outlet of the secondary wet deacidification tower is connected with the flue gas inlet of the wet electrostatic precipitator, the flue gas outlet of the wet electrostatic precipitator is connected with the raw flue gas inlet of the GGH flue gas heat exchanger, the raw flue gas outlet of the GGH flue gas heat exchanger is connected with the flue gas inlet of the SGH flue gas reheater, the flue gas outlet of the SGH flue gas reheater is connected with the flue gas inlet of the SCR denitration device, the flue gas outlet of the SCR denitration device is connected with the clean flue gas inlet of the GGH flue gas heat exchanger, the clean flue gas outlet of the GGH flue gas heat exchanger is connected with the flue gas inlet of the induced draft fan, and the flue gas is pressurized by the induced draft fan and then discharged into the atmosphere through the chimney, so that the standard-reaching discharge of the waste gas is realized.
An organic hazardous waste integrated plasma multi-stage gasification melting furnace method is characterized by comprising but not limited to the following steps:
the method comprises the following steps: organic hazardous wastes enter the counter-current rotary type primary gasification furnace from the kiln tail cover through the organic hazardous waste spiral feeding device, and the organic hazardous wastes and combustion air move in opposite directions; the hazardous waste spiral feeding device adopts frequency conversion control and adjusts the feeding rate; the burner automatically controls the flow of the auxiliary fuel to adjust the gasification reaction temperature in the furnace; the primary gasification fan controls and adjusts the primary gasification air quantity in a frequency conversion way, so that the horizontal rotary kiln forms an obvious oxygen concentration gradient along the axial direction; the rotary driving system of the counter-current rotary type primary gasification furnace adopts variable frequency control to adjust the gasification reaction time of the hazardous waste; when multiple types and complex components of organic hazardous wastes are comprehensively gasified, the feeding rate (spiral frequency), the primary gasification air quantity, the auxiliary fuel quantity, the gasification temperature-1000 ℃, the gasification reaction time (rotation driving frequency of a counter-current rotary primary gasification furnace), the oxygen content of synthesis gas is 0.2-1%, and the CO concentration of the synthesis gas is 7-12% by controlling and adjustingSynthesis gas CH 4 The process conditions and the operation parameters such as concentration (within 1 percent) and the like enable the organic hazardous waste to undergo the processes of drying, fast pyrolysis, fast gasification and the like in a primary gasification furnace, and completely convert organic matters with high boiling points, macromolecular chains and difficult decomposition into H 2 CO and CH 4 The problems of slow reaction, incomplete reaction, equipment blockage caused by tar and pollution caused by dioxin in the traditional pyrolysis gasification process are fundamentally solved by combustible gas (synthesis gas), and meanwhile, a small amount of solid semicoke containing fixed carbon and inorganic matters is generated by the primary gasification furnace; the synthesis gas enters a secondary combustion chamber through a synthesis gas outlet pipeline of the kiln tail cover for gaseous homogeneous combustion, which is beneficial to efficient recovery and utilization of waste heat; the solid semi-coke falls into the vertical secondary gasification furnace along with the rotation of the counter-current rotary primary gasification furnace for further treatment;
step two: solid semicoke generated by pyrolysis and gasification of the countercurrent rotary type primary gasification furnace forms a material bed layer with a certain height in the vertical type secondary gasification furnace, the fluxing agent and the coke are fed into the vertical type secondary gasification furnace through a fluxing agent feeding device, the coke is converged between the material bed layer and the molten slurry to form a coke bed layer due to the specific gravity difference, the coke bed layer provides support for the material bed layer and guides plasma jet distribution into the material bed layer, and the coke bed layer provides a gap for downward flow of glassy state slag and metal objects; the high temperature and high reaction activity of the plasma enable the fixed carbon in the solid semicoke to be rapidly gasified into CO, the plasma high-temperature rapid gasification of the solid semicoke is realized by controlling and adjusting the process conditions and the operation parameters such as the plasma torch power, the secondary gasification air quantity, the secondary gasification temperature and the like, the defects of slow reaction process and incomplete reaction of the solid semicoke in the traditional thermochemical treatment technology are overcome, the precondition of dioxin synthesis is stopped, and the problem of dioxin pollution is eliminated from the source; the ash is melted in the high-temperature gasification process of the plasma, and the ash melting point temperature of the ash can be effectively reduced by adjusting the power of the plasma torch and the type and quantity of the fluxing agent, so that the fluidity of the molten slurry is improved, and the energy consumption of the system is reduced; after accumulating to a certain amount, the slag is discharged out of the furnace through a slag outlet of a molten pool at the bottom of the secondary gasification furnace, and is cooled by water quenching to form a glassy substance; according to the technical requirement for vitrification treatment products of solid wastes (GB/T41015-2021), the glassy substances are used as general solid wastes to realize resource utilization after being inspected to be qualified, so that the generation of secondary dangerous wastes is avoided; the high-temperature synthesis gas generated by the vertical secondary gasification furnace is used as a part of heat source of the counter-flow rotary primary gasification furnace, and the primary gasification reaction process can be obviously enhanced and accelerated. Through the first step and the second step, the segmented and graded gasification of the organic hazardous waste is realized, the adjustment and control of gasification conditions and process parameters are optimized, and the material adaptability and gasification efficiency of the device and the system are obviously improved;
step three: the synthesis gas is efficiently and homogeneously combusted in the secondary combustion chamber, and a large amount of heat can be released without supplementing auxiliary fuel, so that the operating temperature of the secondary combustion chamber is maintained to be more than or equal to 1100 ℃; the heat released by the combustion of the synthesis gas is recovered by a waste heat recovery device for power generation or direct steam utilization, so that the economical efficiency of the system operation can be improved; before the state does not release special technical specifications and pollution control standards for treating hazardous wastes by using a plasma technology, 500 ℃ flue gas after waste heat recovery needs to enter a quenching device to be rapidly cooled to within 200 ℃ within 1 second, and a temperature interval for resynthesis of dioxin is avoided so as to meet the requirements of hazardous waste incineration pollution control standards (GB 18484);
step four: removing part of SO from the flue gas rapidly cooled by the quenching device by a dry deacidification device 2 Heavy metal and dioxin in the fume from dry deacidification are eliminated through active carbon adsorption, most of the particles are eliminated through filtering in a cloth bag dust collector, and SO is eliminated further in the fume from dust collection in pre-cooling tower and two-stage wet deacidification tower 2 The flue gas after wet deacidification is further subjected to particulate matter removal, acid mist removal and salt mist removal through a wet electrostatic precipitator;
step five: outlet flue gas (to 68 ℃) of wet electrostatic dust collection is heated to 140 ℃ through a GGH flue gas heat exchanger, a flue gas outlet of the wet electrostatic dust collector is connected with an original flue gas inlet of the GGH flue gas heat exchanger, a flue gas outlet (to 200 ℃) of an SCR denitration device is connected with a clean flue gas inlet of the GGH flue gas heat exchanger, after heat exchange is carried out between high-temperature flue gas and low-temperature flue gas, the flue gas temperature of the clean flue gas outlet of the GGH flue gas heat exchanger is reduced to about 130 ℃, the flue gas temperature of the original flue gas outlet of the GGH flue gas heat exchanger is increased to about 140 ℃, and the purposes of utilizing the high-temperature flue gas waste heat at the outlet of the SCR denitration device and reducing the energy consumption of a system are achieved;
step six: the gas fume after GGH heating is further heated to about 200 ℃ by an SGH gas fume reheater, and NO is further deeply removed from the gas fume after SGH heating by an SCR catalytic denitration device X Meets the limit requirement of hazardous waste incineration pollution control standard (GB 18484); the SGH flue gas reheater heats the flue gas to 200 ℃ by using 300 ℃ superheated steam generated by the waste heat recovery device so as to meet the requirement of the working temperature of the SCR denitration device;
step seven: and the outlet clean flue gas of the GGH flue gas heat exchanger is pressurized by a draught fan and is discharged into the atmosphere from a chimney.
Compared with the prior rotary kiln incinerator, fixed bed pyrolysis gasifier, plasma pyrolysis furnace, fixed bed plasma gasification and melting integrated furnace and pyrolysis furnace cooperated plasma melting furnace, the invention has the following remarkable effects: by the integrated series application of the countercurrent rotary type first-stage gasification furnace and the vertical type second-stage gasification furnace (plasma high-temperature gasification), the organic hazardous waste is gasified in a segmented and graded manner, the technical defect that the pyrolysis process of a fixed bed plasma gasification melting integrated furnace is slow is overcome, and the material adaptability, reliability and economy of the integrated plasma gasification melting device are obviously enhanced; the countercurrent rotary type primary gasification furnace is arranged to carry out high-temperature pyrolysis gasification on volatile matters of the organic hazardous wastes, and the vertical type secondary gasification furnace is arranged to carry out plasma high-temperature gasification on the solid semicoke, so that the problem that the regulation and control of the reaction process of the rotary kiln incinerator, the fixed bed pyrolysis gasification furnace, the plasma pyrolysis furnace and the fixed bed plasma gasification and melting integrated furnace are difficult is solved, the organic matter pyrolysis gasification process and the solid semicoke gasification process are enhanced, the reaction process is fast, the reaction is more thorough, the pollutant discharge is low, the gasification efficiency is high, and the equipment is easy to amplify; by arranging the plasma torch and the secondary gasification wind, the advantages of high temperature and high reaction activity of the plasma are utilized, the solid-state semicoke gasification process is fast, the fixed carbon is thoroughly gasified, and the ash content is melted in the high-temperature semicoke gasification process, so that the defect that the plasma is used as a high-temperature heat source in a plasma pyrolysis furnace and a plasma melting furnace is overcome, the energy consumption of the device and the system is reduced, and the running economy of the device is obviously enhanced; meanwhile, the problems that the semicoke gasification combustion process of the rotary kiln incinerator and the fixed bed pyrolysis gasifier is slow, the reaction is not thorough, the thermal ignition reduction rate of the residues is high, the carbon content of the residues is high, the quantity of the residues is large, and the residues still belong to hazardous waste are solved, and the harmlessness and the reduction of the organic hazardous waste are thoroughly realized; the plasma multistage gasification melting device is high in gasification efficiency and good in combustibility of synthesis gas, the synthesis gas is efficiently and homogeneously combusted in the secondary combustion chamber, a large amount of heat can be released without supplementing auxiliary fuel, the operating temperature of the secondary combustion chamber is maintained to be more than or equal to 1100 ℃, the heat released by combustion of the synthesis gas is recycled by a waste heat recovery device for power generation or direct steam utilization, and the waste energy conversion efficiency of the plasma multistage gasification melting device is remarkably higher than that of a rotary kiln incinerator, a fixed bed gasification pyrolysis furnace, a plasma pyrolysis furnace, a fixed bed plasma gasification melting integrated furnace and a plasma melting furnace.
Drawings
FIG. 1 is a schematic view of an integrated plasma multi-stage gasification melting furnace device for hazardous organic waste according to the present invention.
FIG. 2 is a schematic view of the kiln tail side of the integrated plasma multi-stage gasification melting furnace device for organic hazardous wastes.
FIG. 3 is a schematic view of the kiln head side of the integrated plasma multi-stage gasification melting furnace device for hazardous organic waste of the present invention.
FIG. 4 is a schematic sectional view of an integrated hazardous organic waste plasma multi-stage gasification melting furnace apparatus A-A according to the present invention.
FIG. 5 is a schematic view of an organic hazardous waste integrated plasma multi-stage gasification melting furnace system of the present invention.
In the figure: 1-a counter-current rotary primary gasification furnace, 2-a vertical secondary gasification furnace and 3-a molten pool; 4-horizontal rotary furnace body, 5-corundum mullite firebrick, 6-kiln tail cover, 7-kiln head cover, 8-synthetic gas outlet pipeline, 9-emergency chimney, 10-organic hazardous waste spiral feeding device, 101-organic hazardous waste spiral feeding port, 11-primary gasification fan, 111-primary gasification tangential air inlet pipe, 12-burner, 121-burner interface, 13-burner fan, 14-kiln tail sealing system, 15-kiln head sealing system, 16-oxygen meter, 17-synthetic gas component analyzer and 18-kiln head sight glass; 19-a vertical cylindrical furnace body, 20-chromium corundum refractory bricks, 21-a plasma torch, 22-a fluxing agent feeding device, 221-a fluxing agent feeding hole, 23-a secondary gasification fan, 231-a secondary gasification annular air pipe, 24-a flange and 25-a viewing mirror; 26-chrome zirconium corundum refractory brick, 27-flat cylinder, 28-slag hole and 29-flange.
To elaborate on technical solutions adopted by the present invention to achieve predetermined technical objects, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, it is obvious that the described embodiments are only partial embodiments of the present invention, not all embodiments, and technical means or technical features in the embodiments of the present invention may be replaced without creative efforts, and the present invention will be described in detail below with reference to the drawings and in conjunction with the embodiments.
As shown in fig. 1, 2, 3 and 4, the integrated hazardous organic waste plasma multi-stage gasification melting furnace device of the present invention includes a counter-current rotary type first-stage gasification furnace 1, a vertical type second-stage gasification furnace 2, a molten pool 3, a hazardous organic waste screw feeder 10, a flux feeder 22, a burner 12, a plasma torch 21, a first-stage gasification fan 11, a second-stage gasification fan 23, an oxygen meter 16 and a syngas component analyzer 17. The countercurrent rotary type primary gasification furnace 1 is connected with the vertical secondary gasification furnace 2 through a kiln hood 7, and the vertical secondary gasification furnace 2 is connected with the molten pool 3, so that an integrated plasma multistage gasification melting device is formed; the connecting part of the kiln head cover 7 and the vertical secondary gasification furnace 2 and the connecting part of the vertical secondary gasification furnace 2 and the molten pool 3 are respectively connected by flanges 24 and 29, so that the maintenance and the overhaul of the refractory material of the device are facilitated. The organic hazardous waste spiral feeding device 10 is connected with the kiln tail cover 6 of the countercurrent rotary type primary gasification furnace, the organic hazardous waste is conveyed by the spiral feeding device 10 and controls the feeding amount of the organic hazardous waste in unit time, the organic hazardous waste enters the countercurrent rotary type primary gasification furnace 1 and is opposite to the high-temperature synthesis gasThe movement and the heat and mass transfer effect in the furnace are good, and the organic hazardous waste is subjected to the processes of drying, fast pyrolysis, fast gasification and the like in sequence; the burner 12 is arranged in the middle of the panel of the reverse-flow rotary primary gasifier kiln hood 7, adopts a split structure, forms a control loop with the first temperature sensor, automatically adjusts the flow of auxiliary fuel such as diesel oil or natural gas and the flow of combustion air conveyed by the burner fan 13, and is used for controlling the temperature of the device during startup and shutdown and adjusting the temperature of the primary gasifier during normal operation; the primary gasification fan 11 is connected with a kiln head cover 7 of the counter-current rotary primary gasification furnace through a primary gasification tangential air inlet pipe 111, primary gasification air tangentially enters the kiln head cover to improve the air turbulence degree in the primary gasification furnace, and primary gasification air quantity and oxygen content are adjusted through frequency conversion of the primary gasification fan; the fluxing agent feeding device 22 is connected with the kiln head cover 7 of the countercurrent rotary type first-stage gasification furnace, the fluxing agent enters the vertical type second-stage gasification furnace from the kiln head cover, and the fluxing agent can adjust the components of the molten slag, reduce the ash melting point temperature and reduce the energy consumption of the system; the plasma torch 21 is positioned at the bottom of the cylinder body of the vertical secondary gasification furnace 2, the plasma torch is matched with a power supply, circulating cooling water and instrument gas (plasma working gas), and the operating power of the plasma torch is adjusted and controlled, so that the gasification process of solid semicoke generated by pyrolysis gasification of the countercurrent rotary primary gasification furnace 1 can be accelerated, the gasification efficiency of the solid semicoke is improved, and the melting temperature (1500 ℃) of inorganic ash and the fluidity of molten slag can be improved; the secondary gasification fan 23 is connected with the bottom of the vertical secondary gasification furnace 2 through at least eight secondary gasification annular air pipes 231, and the secondary gasification air quantity and the oxygen content are adjusted through the secondary gasification fan in a frequency conversion mode; the oxygen measuring instrument 16 is positioned at the horizontal part of the synthesis gas outlet pipeline 8 of the counter-current rotary primary gasification furnace 1, monitors the oxygen content (0.2-1%) of the synthesis gas, and is used for feeding back and adjusting the air supply quantity and distribution of the primary gasification fan and the secondary gasification fan so as to ensure that the integrated device is in an economic and efficient oxygen control gasification operation state; the synthesis gas component analyzer 17 is positioned at the horizontal part of the synthesis gas outlet pipeline 8 of the counter-current rotary type first-stage gasification furnace 1 and is used for monitoring and controlling the heat value of the synthesis gas and CO and H 2 、CH 4 The content, CO concentration is controlled to be 7% -12%, and CH 4 The concentration is controlled to be 1Within%, the device is ensured to be in a safe and reliable operation state.
The counter-current rotary primary gasification furnace 1 comprises a horizontal rotary furnace body 4, refractory materials 5, a kiln tail cover 6, a kiln head cover 7, a synthetic gas outlet pipeline 8, an emergency chimney 9, a kiln tail sealing system 14, a kiln head sealing system 15 and a kiln head sight glass 18; the included angle between the axis of the horizontal rotary furnace body 4 and the horizontal direction is 2-4 degrees; the refractory material 5 is a refractory brick made of corundum-mullite; the joint of the horizontal rotary furnace body 4, the kiln tail cover 6 and the kiln head cover 7 forms a double-sealing system by arranging a kiln tail sealing system 14 and a kiln head sealing system 15, so that the air leakage quantity of the counter-current rotary primary gasification furnace 1 is controlled within 2 percent; the emergency chimney 9 and the synthetic gas outlet pipeline 8 are arranged on the kiln tail cover 6 in a centralized way; a synthetic gas outlet pipeline 8 is connected with an inlet of the secondary combustion chamber through a pipeline led out from an emergency chimney 9 through a tee joint; the kiln head sight glass 18 is arranged on the kiln head cover panel and is intersected with the axial center line of the horizontal rotary furnace body 4, so that the gasification reaction process of the organic hazardous waste in the primary gasification furnace can be observed conveniently, and the auxiliary adjustment of the process conditions and the operation parameters of the primary gasification can be facilitated.
The vertical secondary gasification furnace 2 comprises a vertical cylindrical furnace body 19, a refractory material 20 and a sight glass 25; the top end of the vertical cylindrical furnace body 19 is connected with the bottom of the kiln head cover 7 of the counter-current rotary primary gasification furnace 1 through a flange 24; the refractory material 20 is a refractory brick made of chrome corundum; the sight glass 25 is arranged at the lower part of the vertical cylindrical furnace body 19, so that the plasma high-temperature gasification and inorganic ash fusion processes of the primary gasification solid semicoke in the secondary gasification furnace can be observed conveniently, and the auxiliary adjustment of the secondary gasification and fusion process conditions and the operation parameters is facilitated.
The molten bath 3 comprises a flat cylindrical body 27, refractory material 26 and a slag outlet 28; the top end of the flat cylinder 27 is connected with the bottom end of the vertical secondary gasification furnace 2 through a flange 29; the refractory 26 is made of a refractory brick made of chrome-zirconia-corundum material which is resistant to erosion by molten slag.
A kiln tail hood 6 and a kiln head hood 7 of the countercurrent rotary type primary gasification furnace 1 are respectively provided with a first temperature sensor and a second temperature sensor, and the bottom of the vertical secondary gasification furnace 2 is provided with a third temperature sensor. The first temperature sensor is used for monitoring the kiln tail operation temperature of the counter-flow rotary type primary gasification furnace 1 so as to adjust the operation power of the burner and the primary gasification air quantity, thereby controlling the primary gasification reaction temperature of the counter-flow rotary type primary gasification furnace; the second temperature sensor is used for monitoring the kiln head operating temperature of the countercurrent rotary type primary gasification furnace 1, and the second temperature sensor and the first temperature sensor share the function of judging and determining the change trend of the gasification characteristics of the organic hazardous waste so as to adjust the rotating speed of the countercurrent rotary type primary gasification furnace, thereby controlling the primary gasification reaction time of the organic hazardous waste and optimizing the process conditions (the feeding rate of the hazardous waste, the power of a burner and the air supply amount); the third temperature sensor is used for monitoring the gasification melting temperature of the vertical secondary gasification furnace 2 so as to adjust the operation power of the plasma and the secondary gasification air volume.
A kiln tail cover 6 and a kiln head cover 7 of the counter-current rotary type primary gasification furnace 1 are respectively provided with a first pressure sensor and a second pressure sensor; the vertical secondary gasification furnace 2 is provided with a third pressure sensor. The first pressure sensor is used for monitoring the micro negative pressure of a kiln tail cover 6 of the counter-flow rotary type primary gasification furnace 1, the second pressure sensor is used for monitoring the micro negative pressure of a kiln head cover 7 of the counter-flow rotary type primary gasification furnace 1, and the third pressure sensor is used for monitoring the micro negative pressure of the vertical type secondary gasification furnace 1 so as to adjust the induced air quantity of the system and ensure that the device operates in a negative pressure closed state; if positive pressure of 100Pa occurs in the furnace, the emergency chimney can be automatically opened through the pneumatic valve, and the system is ensured to run in a safe state.
An organic hazardous waste integrated plasma multi-stage gasification melting furnace system comprises an organic hazardous waste pretreatment system, an integrated plasma multi-stage gasification melting furnace device, a secondary combustion chamber, a waste heat recovery device, a flue gas purification device, an induced draft fan, a chimney, a fly ash collection system, a sewage treatment system and the like, wherein a discharge port of the pretreatment system is connected with a feed inlet of an organic hazardous waste spiral feeding device and/or a fluxing agent feeding device of the integrated plasma multi-stage gasification melting furnace device for organic hazardous waste, a synthetic gas outlet pipeline of the integrated plasma multi-stage gasification melting furnace device for organic hazardous waste is connected with a flue gas inlet of the secondary combustion chamber, a flue gas outlet of the secondary combustion chamber is connected with a flue gas inlet of the waste heat recovery device, a flue gas outlet of the waste heat recovery device is connected with a flue gas inlet of the flue gas purification device, a flue gas outlet of the flue gas purification device is connected with a flue gas inlet of the induced draft fan, the smoke outlet of the induced draft fan is connected with the inlet of the chimney, and the emission of the waste gas reaching the standard is finally realized; fly ash generated by the waste heat recovery device and the flue gas purification device is collected, granulated and pretreated, then returned to the vertical secondary gasification furnace by the fluxing agent feeding device for melting treatment, and the production wastewater of the waste heat recovery device and the flue gas purification device is lifted to a sewage treatment system for treatment by a pump. Carrying out multi-stage gasification and melting treatment on the organic hazardous waste by using plasma to generate synthesis gas and glassy slag; the glassy slag can be used as a general building material or used in a high-value way; the synthesis gas enters a secondary combustion chamber for high-efficiency combustion (the combustion temperature is more than or equal to 1100 ℃), the combustion flue gas enters a membrane wall boiler waste heat recovery device, the waste heat is recovered, the temperature is reduced to 500 ℃, and then the temperature is reduced to be within 200 ℃ through a quenching device, so that the temperature range of the dioxin resynthesis is avoided.
The flue gas purification device comprises an SNCR (selective non-catalytic reduction) denitration device, a quenching device, a dry deacidification device, an activated carbon injection device, a cloth bag dust removal device, a pre-cooling tower, a two-stage wet deacidification tower, a wet electrostatic dust removal device, a GGH (gas-gas heater) flue gas heat exchanger, an SGH flue gas reheater and an SCR (selective catalytic reduction) denitration device which are arranged at a flue gas high-temperature section (850-1100 ℃) of the waste heat recovery device; the waste heat recovery device is provided with an SNCR denitration device at the high-temperature section (850 ℃ -1100 ℃) of the flue gas, and a 10% urea solution is metered and sprayed by a two-fluid spray gun, so that NO in the flue gas X Is selectively reduced to N without catalysis 2 The denitration efficiency is not lower than 40%; a flue gas outlet of the waste heat recovery device is connected with a flue gas inlet of a quenching device, quenching water is pumped to a double-fluid spray gun at the upper part of a quenching tower, and the quenching water is atomized into small-particle atomized water of 40 micrometers by compressed air and then sprayed into the quenching tower to be fully contacted with the flue gas, so that the flue gas is rapidly cooled to 200 ℃ within 1s, and a temperature range (500-200 ℃) for resynthesis of the dioxin in the flue gas is avoided; the flue gas outlet of the quenching device and the activated carbon outlet of the activated carbon injection device are connected with the flue gas inlet of the dry deacidification device, the dry deacidification device is provided with a Venturi tube type mixer, slaked lime and activated carbon are fully mixed with flue gas through the Venturi tube type mixer, and HCl and SO in the flue gas 2 HF and other acidic gasesLime generates neutralization reaction, the removal rate of acid gas is not less than 20%, and dioxin and partial volatile heavy metal in the flue gas are removed by adsorption of activated carbon; the flue gas outlet of the dry deacidification device is connected with the flue gas inlet of the bag-type dust removal device, particulate matters in the flue gas are filtered by the bag-type dust removal device to be removed, most heavy metals (such as lead, cadmium and the like exist in a solid form below 300 ℃) are agglomerated with the particulate matters to be removed by the bag-type dust removal device, and the concentration of the flue gas particulate matters after the bag-type dust removal is less than 10mg/m 3 (ii) a The flue gas outlet of the cloth bag dust removal device is connected with the flue gas inlet of the pre-cooling tower, and the temperature of the flue gas is reduced to-71 ℃ through a pre-cooling water spray gun arranged at the flue gas inlet of the pre-cooling tower, so that the purposes of reducing the temperature and humidifying the flue gas are achieved; the flue gas outlet of the pre-cooling tower is connected with the flue gas inlet of the first-stage wet deacidification tower, and the flue gas is in countercurrent contact with the circulating alkali liquor and generates a neutralization reaction, so that most of acid gas in the flue gas is removed; the flue gas outlet of the first-stage wet deacidification tower is connected with the flue gas inlet of the second-stage wet deacidification tower, and residual acid gas in the flue gas continuously contacts with circulating alkali liquor in a countercurrent manner and generates a neutralization reaction so as to ensure that the wet deacidification tower runs reliably, the wet deacidification efficiency can reach 99 percent, and the emission limit value requirement of hazardous waste incineration pollution control standard (GB 18484) is met; most of volatile heavy metals such as mercury and the like with high saturated vapor pressure exist in the flue gas in a gaseous state, and in the processes of precooling and wet deacidification, mercury in the flue gas can react with HCl, 80-90% of mercury can be converted into HgCl 2 ，HgCl 2 Is a water-soluble compound, HgCl 2 Reacting with circulating alkali liquor to remove; the flue gas outlet of the second-stage wet-type deacidification tower is connected with the flue gas inlet of the wet-type electrostatic dust removal device, the wet-type electrostatic dust removal device has certain dust removal capacity, the ultra-low emission of particulate matters can be realized by cooperating with a bag-type dust remover, and the wet-type electrostatic demister can effectively remove salt mist and acid mist in the flue gas to avoid poisoning and inactivation of a catalyst of a subsequent SCR denitration device; in order to meet the denitration temperature requirement (200 ℃) of a subsequent SCR denitration device, outlet flue gas of a wet electrostatic dust removal device is heated by a GGH flue gas heat exchanger, a flue gas outlet of the wet electrostatic dust removal device is connected with an original flue gas inlet of the GGH flue gas heat exchanger, and a flue gas outlet of the SCR denitration device is connected with the GGH flue gasThe clean flue gas inlet of the heat exchanger is connected, flue gas at the temperature of 200 ℃ of an SCR (selective catalytic reduction) denitration device is used for heating flue gas at the temperature of 68 ℃ below zero at the outlet of the wet electrostatic dust removal device, after heat exchange is carried out between GGH (gas-gas heater) flue gas and flue gas, the temperature of the original flue gas is raised to 140 ℃, and the temperature of the clean flue gas is lowered to 130 ℃, so that the aims of utilizing the waste heat of the flue gas of the SCR denitration device and reducing the energy consumption of a system are fulfilled; the method comprises the following steps of heating raw flue gas at a raw flue gas outlet of a GGH flue gas heat exchanger again by using an SGH flue gas reheater, connecting the raw flue gas outlet of the GGH flue gas heat exchanger with a flue gas inlet of the SGH flue gas reheater, heating the flue gas to 200 ℃ by using superheated steam at 300 ℃ generated by a waste heat recovery device, and meeting the denitration temperature requirement of a subsequent SCR denitration device; the flue gas outlet of the SGH flue gas reheater is connected with the flue gas inlet of an SCR denitration device, and SCR denitration is selective catalytic reduction for removing NO X NO catalyzed by selective low temperature reduction catalyst X And NH 3 Oxidation-reduction reaction is carried out to remove NO in the flue gas X Selective catalytic reduction to N 2 Realization of NO X Discharging after reaching the standard; the flue gas outlet of the SCR denitration device is connected with the clean flue gas inlet of the GGH flue gas heat exchanger, the flue gas temperature at the SCR denitration outlet is close to 200 ℃, the overhigh flue gas temperature has high requirement on the temperature resistance of subsequent equipment (a fan and a chimney), the equipment investment is directly increased, and the waste heat of the flue gas is wasted, so the GGH flue gas heat exchanger is adopted to recycle the waste heat of the flue gas at the SCR denitration outlet, and the low-temperature raw flue gas at the outlet of the wet electrostatic dust removal device is preheated and heated; and finally, a clean flue gas outlet of the GGH flue gas heat exchanger is connected with an inlet of an induced draft fan, and the clean flue gas is pressurized by the induced draft fan and is discharged into the atmosphere from a chimney.
An organic hazardous waste integrated plasma multi-stage gasification melting furnace method is characterized by comprising but not limited to the following steps:
the method comprises the following steps: organic hazardous wastes enter the counter-current rotary primary gasification furnace from the kiln tail cover through the organic hazardous waste spiral feeding device, and the organic hazardous wastes and combustion-supporting air move in opposite directions; the hazardous waste spiral feeding device adopts frequency conversion control and adjusts the feeding rate; the burner automatically controls the flow of the auxiliary fuel to adjust the gasification reaction temperature in the furnace; frequency conversion control and adjustment of primary gasification air quantity of primary gasification fanSo that the horizontal rotary kiln forms an obvious oxygen concentration gradient along the axial direction; the rotary driving system of the countercurrent rotary type primary gasification furnace adopts variable frequency control to adjust the gasification reaction time of hazardous wastes; when various and complex organic hazardous wastes are comprehensively gasified, the feeding rate (spiral frequency), the primary gasification air quantity, the auxiliary fuel quantity, the gasification temperature-1000 ℃, the gasification reaction time (rotary driving frequency of a counter-current rotary primary gasification furnace), the oxygen content of synthesis gas 0.2-1%, the CO concentration of synthesis gas (7-12%), and the CH content of synthesis gas are controlled and adjusted 4 The process conditions and the operation parameters such as concentration (within 1 percent) and the like enable the organic hazardous waste to undergo the processes of drying, fast pyrolysis, fast gasification and the like in a primary gasification furnace, and completely convert organic matters with high boiling points, macromolecular chains and difficult decomposition into H 2 CO and CH 4 The problems of slow reaction, incomplete reaction, equipment blockage caused by tar and pollution caused by dioxin in the traditional pyrolysis gasification process are fundamentally solved by combustible gas (synthesis gas), and meanwhile, a small amount of solid semicoke containing fixed carbon and inorganic matters is generated by the primary gasification furnace; the synthesis gas enters a secondary combustion chamber through a synthesis gas outlet pipeline of the kiln tail cover for gaseous homogeneous combustion, which is beneficial to efficient recovery and utilization of waste heat; the solid semicoke falls into the vertical secondary gasification furnace along with the rotation of the counter-current rotary primary gasification furnace for further treatment;
step two: solid semicoke generated by pyrolysis and gasification of the counter-current rotary type primary gasification furnace forms a material bed layer with a certain height in the vertical type secondary gasification furnace, a fluxing agent and coke are fed into the vertical type secondary gasification furnace through a fluxing agent feeding device, the coke is converged between the material bed layer and molten slurry through specific gravity difference to form a coke bed layer, the coke bed layer provides support for the material bed layer and guides plasma jet distribution into the material bed layer, and the coke bed layer provides a gap for downward flow of glassy-state slag and metal objects; the high temperature and high reaction activity of the plasma enable the fixed carbon in the solid semicoke to be rapidly gasified into CO, the plasma high-temperature rapid gasification of the solid semicoke is realized by controlling and adjusting the process conditions and the operation parameters such as the plasma torch power, the secondary gasification air quantity, the secondary gasification temperature and the like, the defects of slow reaction process and incomplete reaction of the solid semicoke in the traditional thermochemical treatment technology are overcome, the precondition of dioxin synthesis is stopped, and the problem of dioxin pollution is eliminated from the source; the ash is melted in the high-temperature gasification process of the plasma, and the ash melting point temperature of the ash can be effectively reduced by adjusting the power of the plasma torch and the type and quantity of the fluxing agent, so that the fluidity of the molten slurry is improved, and the energy consumption of the system is reduced; after accumulating to a certain amount, the slag is discharged out of the furnace through a slag outlet of a molten pool at the bottom of the secondary gasification furnace, and is cooled by water quenching to form a glassy substance; according to the technical requirement for vitrification treatment products of solid wastes (GB/T41015-2021), the glass-state substances are used as general solid wastes to realize resource utilization after being inspected to be qualified, so that the generation of secondary dangerous wastes is avoided; the high-temperature synthesis gas generated by the vertical secondary gasification furnace is used as a part of heat source of the counter-flow rotary primary gasification furnace, and the primary gasification reaction process can be obviously enhanced and accelerated. Through the first step and the second step, the segmented and graded gasification of the organic hazardous waste is realized, the adjustment and control of gasification conditions and process parameters are optimized, and the material adaptability and gasification efficiency of the device and the system are obviously improved;
step three: the synthesis gas is efficiently and homogeneously combusted in the secondary combustion chamber, and a large amount of heat can be released without supplementing auxiliary fuel, so that the operating temperature of the secondary combustion chamber is maintained to be more than or equal to 1100 ℃; the heat released by the combustion of the synthesis gas is recovered by a waste heat recovery device for power generation or direct steam utilization, so that the economical efficiency of the system operation can be improved; before the state does not release special technical specifications and pollution control standards for treating hazardous wastes by using a plasma technology, 500 ℃ flue gas after waste heat recovery needs to enter a quenching device to be rapidly cooled to within 200 ℃ within 1 second, and a temperature interval for resynthesis of dioxin is avoided so as to meet the requirements of hazardous waste incineration pollution control standards (GB 18484);
step four: removing part of SO from the flue gas rapidly cooled by the quenching device by a dry deacidification device 2 Heavy metal and dioxin in the fume from dry deacidification are eliminated through active carbon adsorption, most of the particles are eliminated through filtering in a cloth bag dust collector, and SO is eliminated further in the fume from dust collection in pre-cooling tower and two-stage wet deacidification tower 2 Acid gases such as HCl and HF, etc.,further removing particulate matters, acid mist and salt mist from the flue gas subjected to wet deacidification by using a wet electrostatic precipitator;
step five: outlet flue gas (to 68 ℃) of wet electrostatic dust collection is heated to 140 ℃ through a GGH flue gas heat exchanger, a flue gas outlet of the wet electrostatic dust collector is connected with an original flue gas inlet of the GGH flue gas heat exchanger, a flue gas outlet (to 200 ℃) of an SCR denitration device is connected with a clean flue gas inlet of the GGH flue gas heat exchanger, after heat exchange is carried out between high-temperature flue gas and low-temperature flue gas, the flue gas temperature of the clean flue gas outlet of the GGH flue gas heat exchanger is reduced to about 130 ℃, the flue gas temperature of the original flue gas outlet of the GGH flue gas heat exchanger is increased to about 140 ℃, and the purposes of utilizing the high-temperature flue gas waste heat at the outlet of the SCR denitration device and reducing the energy consumption of a system are achieved;
step six: the method comprises the steps that the gas fume heated by GGH is further heated to 200 ℃ through an SGH gas fume reheater, and NO is further deeply removed from the gas fume heated by SGH through an SCR catalytic denitration device X Meets the limit requirements of hazardous waste incineration pollution control standard (GB 18484); the SGH flue gas reheater heats the flue gas to 200 ℃ by using 300 ℃ superheated steam generated by the waste heat recovery device so as to meet the requirement of the working temperature of the SCR denitration device;
step seven: and the clean flue gas at the outlet of the GGH flue gas heat exchanger is pressurized by a draught fan and is discharged into the atmosphere from a chimney.
The invention discloses an integrated multistage gasification melting furnace device, system and method for organic hazardous wastes, comprising a counter-current rotary primary gasification furnace, a vertical secondary gasification furnace, a molten pool, a hazardous waste spiral feeding device, a fluxing agent feeding device, a burner, a plasma torch, a primary gasification fan, a secondary gasification fan, an oxygen measuring instrument and a synthesis gas component analyzer; the countercurrent rotary type primary gasification furnace comprises a horizontal rotary furnace body, refractory materials, a kiln tail cover, a kiln head cover, a synthetic gas outlet pipeline, an emergency chimney, a kiln tail sealing system, a kiln head sealing system and a sight glass; the vertical secondary gasification furnace comprises a vertical cylindrical furnace body, a refractory material and a sight glass; the molten pool comprises a flat cylinder, refractory materials and a slag outlet; the device comprises a hazardous waste spiral feeding device, a fluxing agent feeding device, a burner, a plasma torch, a first-stage gasification fan, a circular kiln hood, a second-stage gasification fan, an oxygen measuring instrument and a synthetic gas component analyzer, wherein the hazardous waste spiral feeding device is connected with a kiln tail hood of a reverse-flow rotary type first-stage gasification furnace, the fluxing agent feeding device is connected with a kiln hood of the reverse-flow rotary type first-stage gasification furnace, the burner is arranged in the middle of a kiln hood panel of the reverse-flow rotary type first-stage gasification furnace, the plasma torch is arranged at the bottom of a cylinder body of a vertical second-stage gasification furnace, the first-stage gasification fan is connected with the circular kiln hood of the reverse-flow rotary type first-stage gasification furnace through an air pipe, the second-stage gasification fan is connected with the bottom of the vertical second-stage gasification furnace through an annular air pipe, the oxygen measuring instrument is arranged on a synthetic gas outlet horizontal pipeline of the reverse-flow rotary type first-stage gasification furnace, and the synthetic gas component analyzer is arranged on a synthetic gas outlet horizontal pipeline of the reverse-flow rotary type first-stage gasification furnace. The invention realizes the segmented and graded gasification of the organic hazardous wastes, strengthens the regulation and control of the gasification process of various organic hazardous wastes, improves the material universality of the device and the system, has the gasification efficiency remarkably higher than that of the traditional pyrolysis gasifier, and has good pollution-reducing and carbon-reducing effects; the ash content melting is realized in the gasification process, the installation and operation power of the plasma torch is greatly reduced, and the investment and operation cost of the industrial application of the plasma gasification melting are effectively reduced.
Although the present invention has been described with reference to the preferred embodiments, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted for elements thereof without departing from the scope of the present invention.
In the description of the present invention, it should be noted that the terms "bottom", "side wall", "top" and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, which are only for the purpose of simplifying the description of the present invention, and do not mean that the parts or devices to be referred to must have specific orientations or positions, and are constructed and operated as specific orientations and positions, and thus, should not be construed as being limited thereto.
Furthermore, the terms "first", "second" and "third" are used merely to facilitate the description of the present invention and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated, whereby the features defined as "first", "second" and "third" may explicitly or implicitly include at least one such feature.
In the present invention, unless otherwise explicitly specified or limited, the terms "connected", "disposed", and the like should be broadly construed, and unless otherwise explicitly limited, the meaning of the above terms in the present invention can be understood by those of ordinary skill in the art in conjunction with the specific context.

Claims (12)

1. The utility model provides a multistage gasification melting furnace device of organic hazardous waste integral type plasma which characterized in that: the system comprises a counter-current rotary primary gasification furnace, a vertical secondary gasification furnace, a molten pool, an organic hazardous waste spiral feeding device, a fluxing agent feeding device, a burner, a plasma torch, a primary gasification fan, a secondary gasification fan, an oxygen meter and a synthesis gas component analyzer.
2. The integrated plasma multi-stage gasification melting furnace device for hazardous organic wastes according to claim 1, characterized in that: the countercurrent rotary type primary gasification furnace comprises a horizontal rotary furnace body, refractory materials, a kiln tail cover, a kiln head cover, a synthetic gas outlet pipeline, an emergency chimney, a kiln tail sealing system, a kiln head sealing system and a kiln head sight glass; the included angle between the axis of the horizontal rotary furnace body and the horizontal direction is 2-4 degrees; the refractory material is a refractory brick made of corundum-mullite material; the joint of the horizontal rotary furnace body, the kiln tail cover and the kiln head cover forms a double-sealing system through a kiln tail sealing system and a kiln head sealing system, so that the air leakage of the primary gasification furnace is controlled within 2%; the emergency chimney and the synthesis gas outlet are arranged on the kiln tail cover in a centralized manner; the synthesis gas outlet is arranged at the top of the kiln tail cover and is connected with the inlet of the secondary combustion chamber through a pipeline; the kiln head sight glass is arranged on the kiln head cover panel and is intersected with the axial center line of the horizontal rotary furnace body, so that the gasification reaction process of the organic hazardous waste in the primary gasification furnace can be observed conveniently, and the auxiliary adjustment of the primary gasification process conditions and the operation parameters is facilitated.
3. The integrated plasma multi-stage gasification melting furnace device for hazardous organic wastes according to claim 1, characterized in that: the vertical secondary gasification furnace comprises a vertical cylindrical furnace body, a refractory material and a sight glass; the top end of the vertical cylindrical furnace body is connected with the bottom of a kiln head cover of the primary gasification furnace in a flange mode; the refractory material is a refractory brick made of chrome corundum; the sight glass is arranged at the lower part of the vertical cylindrical furnace body, so that the plasma high-temperature gasification and inorganic ash fusion processes of the primary gasification solid semicoke in the secondary gasification furnace can be observed conveniently, and the auxiliary adjustment of secondary gasification and fusion process conditions and operation parameters is facilitated.
4. The integrated plasma multi-stage gasification melting furnace device for organic hazardous wastes according to claim 1, characterized in that: the molten pool comprises a flat cylinder, refractory materials and a slag outlet; the top end of the flat cylinder is connected with the bottom end of the secondary gasification furnace in a flange mode; the refractory material is a refractory brick made of chrome-zirconium corundum and used for preventing molten slag corrosion.
5. The integrated plasma multi-stage gasification melting furnace device for hazardous organic wastes according to claim 1, characterized in that: the spiral feeding device for the organic hazardous wastes is connected with a kiln tail cover of the countercurrent rotary type primary gasification furnace; the fluxing agent feeding device is connected with a kiln hood of the counter-current rotary type primary gasification furnace; the burner is arranged in the middle of a face plate of a kiln head cover of the counter-flow rotary type primary gasification furnace; the plasma torch is positioned at the bottom of the cylinder body of the vertical secondary gasification furnace; the primary gasification fan is connected with a circular kiln hood of the counter-current rotary primary gasification furnace through an air pipe, primary gasification air tangentially enters the kiln hood, and the air turbulence degree in the primary gasification furnace is improved; the secondary gasification fan is connected with the bottom of the vertical secondary gasification furnace through at least eight annular air pipes; the oxygen measuring instrument is positioned on a horizontal pipeline of a synthetic gas outlet of the countercurrent rotary type primary gasification furnace; the synthesis gas component analyzer is positioned on a horizontal pipeline of a synthesis gas outlet of the counter-current rotary type primary gasification furnace.
6. The integrated plasma multi-stage gasification melting furnace device for hazardous organic wastes according to claim 1, characterized in that: a kiln tail cover and a kiln head cover of the countercurrent rotary type primary gasification furnace are respectively provided with a first temperature sensor and a second temperature sensor; and a third temperature sensor is arranged at the bottom of the vertical secondary gasification furnace.
7. The integrated plasma multi-stage gasification melting furnace device for hazardous organic wastes according to claim 1, characterized in that: a kiln tail cover and a kiln head cover of the countercurrent rotary type primary gasification furnace are respectively provided with a first pressure sensor and a second pressure sensor; the vertical secondary gasification furnace is provided with a third pressure sensor.
8. The integrated plasma multi-stage gasification melting furnace device for hazardous organic wastes according to claim 5, wherein: and the primary gasification fan and the secondary gasification fan are controlled by frequency conversion.
9. The integrated plasma multi-stage gasification melting furnace device for hazardous organic wastes according to claim 5, wherein: the combustor adopts a split type structure, and the combustor and the first temperature sensor form a control loop to automatically adjust the flow of auxiliary fuel such as diesel oil or natural gas and the flow of combustion-supporting air conveyed by a combustor fan, so that the combustor is used for controlling the temperature of the start-up and shut-down of the device and adjusting the temperature of the gasification process in the primary gasification furnace during normal operation.
10. The utility model provides a multistage gasification melting furnace system of organic hazardous waste integral type plasma which characterized in that: the integrated type plasma multi-stage gasification melting furnace device for organic hazardous wastes, which comprises the integrated type plasma multi-stage gasification melting furnace device for organic hazardous wastes according to any one of claims 1 to 9, further comprises an organic hazardous waste pretreatment system, a secondary combustion chamber, a waste heat recovery device, a flue gas purification device, an induced draft fan, a chimney, a fly ash collection system, a sewage treatment system and the like, wherein a discharge port of the pretreatment system is connected with a feed inlet of an organic hazardous waste spiral feeding device and/or a fluxing agent feeding device of the integrated type plasma multi-stage gasification melting furnace device for organic hazardous wastes, a synthetic gas outlet pipeline of the integrated type plasma multi-stage gasification melting furnace device for organic hazardous wastes is connected with a flue gas inlet of the secondary combustion chamber, a flue gas outlet of the secondary combustion chamber is connected with a flue gas inlet of the waste heat recovery device, a flue gas outlet of the waste heat recovery device is connected with a flue gas inlet of the flue gas purification device, a flue gas outlet of the flue gas purification device is connected with a flue gas inlet of the induced draft fan, the smoke outlet of the induced draft fan is connected with the inlet of the chimney, and finally the emission of the waste gas reaching the standard is realized; fly ash generated by the waste heat recovery device and the flue gas purification device is returned to the vertical secondary gasification furnace for melting treatment by the fluxing agent feeding device after being collected, granulated and pretreated, and production wastewater of the flue gas purification device is lifted to a sewage treatment system for treatment by a pump.
11. The integrated plasma multi-stage gasification melter system of claim 10 wherein: the flue gas purification device comprises an SNCR (selective non-catalytic reduction) denitration device, a quenching device, a dry deacidification device, an activated carbon injection device, a cloth bag dust removal device, a pre-cooling tower, a two-stage wet deacidification tower, a wet electrostatic dust collector, a GGH (gas-gas heater) flue gas heat exchanger, an SGH flue gas reheater and an SCR (selective catalytic reduction) denitration device which are arranged at a high-temperature section (850-1100 ℃) of flue gas of the waste heat recovery device; the flue gas outlet of the quenching device and the material outlet of the activated carbon injection device are connected with the flue gas inlet of the dry deacidification device, the flue gas outlet of the dry deacidification device is connected with the flue gas inlet of the bag-type dust removal device, the flue gas outlet of the bag-type dust removal device is connected with the flue gas inlet of the pre-cooling tower, the flue gas outlet of the pre-cooling tower is connected with the flue gas inlet of the primary wet deacidification tower, the flue gas outlet of the primary wet deacidification tower is connected with the flue gas inlet of the secondary wet deacidification tower, the flue gas outlet of the secondary wet deacidification tower is connected with the flue gas inlet of the wet electrostatic precipitator, the flue gas outlet of the wet electrostatic precipitator is connected with the raw flue gas inlet of the GGH flue gas heat exchanger, the raw flue gas outlet of the GGH flue gas heat exchanger is connected with the flue gas inlet of the SGH flue gas reheater, the flue gas outlet of the SGH flue gas reheater is connected with the flue gas inlet of the SCR denitration device, the flue gas outlet of the SCR denitration device is connected with the clean flue gas inlet of the GGH flue gas heat exchanger, the clean flue gas outlet of the GGH flue gas heat exchanger is connected with the flue gas inlet of the induced draft fan, and the flue gas is pressurized by the induced draft fan and then discharged into the atmosphere through the chimney, so that the standard-reaching discharge of the waste gas is realized.
12. An organic hazardous waste integrated plasma multi-stage gasification melting furnace method is characterized by comprising but not limited to the following steps:
the method comprises the following steps: organic hazardous wastes enter the counter-current rotary primary gasification furnace from the kiln tail cover through the organic hazardous waste spiral feeding device, and the organic hazardous wastes and combustion-supporting air move in opposite directions; the hazardous waste spiral feeding device adopts frequency conversion control and adjusts the feeding rate; the burner automatically controls the flow of the auxiliary fuel to adjust the gasification reaction temperature in the furnace; the primary gasification fan controls and adjusts the primary gasification air quantity in a frequency conversion way, so that the horizontal rotary kiln forms an obvious oxygen concentration gradient along the axial direction; the rotary driving system of the counter-current rotary type primary gasification furnace adopts variable frequency control to adjust the gasification reaction time of the hazardous waste; when various and complex organic hazardous wastes are comprehensively gasified, the feeding rate (spiral frequency), the primary gasification air quantity, the auxiliary fuel quantity, the gasification temperature to 1000 ℃, the gasification reaction time (rotary driving frequency of a counter-current rotary primary gasification furnace), the oxygen content of synthesis gas to be 0.2-1%, the CO concentration of the synthesis gas to be 7-12% and the CH content of the synthesis gas to be synthesized are controlled and adjusted 4 The process conditions and the operation parameters such as concentration (within 1 percent) and the like enable the organic hazardous waste to undergo the processes of drying, fast pyrolysis, fast gasification and the like in a primary gasification furnace, and completely convert organic matters with high boiling points, macromolecular chains and difficult decomposition into H 2 CO and CH 4 The problems of slow reaction, incomplete reaction, equipment blockage caused by tar and dioxin pollution in the traditional pyrolysis gasification process are fundamentally solved by the aid of combustible gas (synthesis gas), and a small amount of solid containing fixed carbon and inorganic matters is generated by the primary gasification furnaceSemi-coke; the synthesis gas enters a secondary combustion chamber through a synthesis gas outlet pipeline of the kiln tail cover for gaseous homogeneous combustion, which is beneficial to efficient recovery and utilization of waste heat; the solid semicoke falls into the vertical secondary gasification furnace along with the rotation of the counter-current rotary primary gasification furnace for further treatment;
step two: solid semicoke generated by pyrolysis and gasification of the counter-current rotary type primary gasification furnace forms a material bed layer with a certain height in the vertical type secondary gasification furnace, a fluxing agent and coke are fed into the vertical type secondary gasification furnace through a fluxing agent feeding device, the coke is converged between the material bed layer and molten slurry through specific gravity difference to form a coke bed layer, the coke bed layer provides support for the material bed layer and guides plasma jet distribution into the material bed layer, and the coke bed layer provides a gap for downward flow of glassy-state slag and metal objects; the high temperature and high reaction activity of the plasma enable the fixed carbon in the solid semicoke to be rapidly gasified into CO, the plasma high-temperature rapid gasification of the solid semicoke is realized by controlling and adjusting the process conditions and the operation parameters such as the plasma torch power, the secondary gasification air quantity, the secondary gasification temperature and the like, the defects of slow reaction process and incomplete reaction of the solid semicoke in the traditional thermochemical treatment technology are overcome, the precondition of dioxin synthesis is stopped, and the problem of dioxin pollution is eliminated from the source; the ash is melted in the high-temperature gasification process of the plasma, and the ash melting point temperature of the ash can be effectively reduced by adjusting the power of the plasma torch and the type and quantity of the fluxing agent, so that the fluidity of the molten slurry is improved, and the energy consumption of the system is reduced; after accumulating to a certain amount, the slag is discharged out of the furnace through a slag outlet of a molten pool at the bottom of the secondary gasification furnace, and is cooled by water quenching to form a glassy substance; according to the technical requirement for vitrification treatment products of solid wastes (GB/T41015-2021), the glass-state substances are used as general solid wastes to realize resource utilization after being inspected to be qualified, so that the generation of secondary dangerous wastes is avoided; the high-temperature synthesis gas generated by the vertical secondary gasification furnace is used as a part of heat source of the counter-flow rotary primary gasification furnace, so that the primary gasification reaction process can be obviously enhanced and accelerated;
through the first step and the second step, the segmented and graded gasification of the organic hazardous waste is realized, the adjustment and control of gasification conditions and process parameters are optimized, and the material adaptability and gasification efficiency of the device and the system are obviously improved;
step three: the synthesis gas is efficiently and homogeneously combusted in the secondary combustion chamber, and a large amount of heat can be released without supplementing auxiliary fuel, so that the operating temperature of the secondary combustion chamber is maintained to be more than or equal to 1100 ℃; the heat released by the combustion of the synthesis gas is recovered by a waste heat recovery device for power generation or direct steam utilization, so that the economical efficiency of the system operation can be improved; before the state does not release special technical specifications and pollution control standards for treating hazardous wastes by using a plasma technology, 500 ℃ flue gas after waste heat recovery needs to enter a quenching device to be rapidly cooled to within 200 ℃ within 1 second, and a temperature interval for resynthesis of dioxin is avoided, so that the requirements of hazardous waste incineration pollution control standards (GB 18484) are met;
step four: removing part of SO from the flue gas rapidly cooled by the quenching device by a dry deacidification device 2 Heavy metal and dioxin are removed from the flue gas after deacidification by a dry method through activated carbon adsorption, most of particles are removed through filtration by a cloth bag dust removal device, and SO is further removed from the flue gas after dust removal through a pre-cooling tower and a two-stage wet type deacidification tower 2 The flue gas after wet deacidification is further subjected to particulate matter removal, acid mist removal and salt mist removal through a wet electrostatic precipitator;
step five: outlet flue gas (to 68 ℃) of wet electrostatic dust collection is heated to 140 ℃ through a GGH flue gas heat exchanger, a flue gas outlet of the wet electrostatic dust collector is connected with an original flue gas inlet of the GGH flue gas heat exchanger, a flue gas outlet (to 200 ℃) of an SCR denitration device is connected with a clean flue gas inlet of the GGH flue gas heat exchanger, after heat exchange is carried out between high-temperature flue gas and low-temperature flue gas, the flue gas temperature of the clean flue gas outlet of the GGH flue gas heat exchanger is reduced to about 130 ℃, the flue gas temperature of the original flue gas outlet of the GGH flue gas heat exchanger is increased to about 140 ℃, and the purposes of utilizing the high-temperature flue gas waste heat at the outlet of the SCR denitration device and reducing the energy consumption of a system are achieved;
step six: the gas after GGH heating is further heated to about 200 ℃ by an SGH gas reheater, and NO is further deeply removed from the gas after SGH heating by an SCR catalytic denitration device X Meets the limit requirement of hazardous waste incineration pollution control standard (GB 18484); SGH flue gas reheatingThe device heats the flue gas to 200 ℃ by using 300 ℃ superheated steam generated by the waste heat recovery device so as to meet the working temperature requirement of the SCR denitration device;
step seven: and the outlet clean flue gas of the GGH flue gas heat exchanger is pressurized by a draught fan and is discharged into the atmosphere from a chimney.
CN202210629984.4A 2022-06-06 2022-06-06 Organic hazardous waste integrated plasma multi-stage gasification melting furnace device, system and method Pending CN115031236A (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116179242A (en) * 2022-12-28 2023-05-30 华电电力科学研究院有限公司 Gasification system for treating hazardous waste by rotary kiln coupling plasma gasification furnace

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116179242A (en) * 2022-12-28 2023-05-30 华电电力科学研究院有限公司 Gasification system for treating hazardous waste by rotary kiln coupling plasma gasification furnace

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