An integrated plasma multi-stage gasification melting furnace device and method for organic hazardous waste

Abstract

The present invention discloses an integrated plasma multi-stage gasification melting furnace device and method for organic hazardous waste, including a countercurrent rotary primary gasifier, a vertical secondary gasifier, a molten pool, a hazardous waste spiral feeding device, a flux feeding device, a burner, a plasma torch, a primary gasification blower, a secondary gasification blower, an oxygen meter and a synthesis gas component analyzer, wherein the burner is used to adjust the temperature of the primary gasifier, and the plasma torch is used to adjust the temperature of the secondary gasifier. The present invention adopts a two-stage gasification treatment, reduces the operating load of the plasma torch and improves the process reliability, thereby reducing the installed capacity and operating power of the plasma torch, significantly enhancing the universality and economy of the integrated plasma gasification melting treatment of organic hazardous waste, and reducing the investment and operation cost of the industrial application of organic hazardous waste plasma gasification melting.

Description

Technical Field

[0001] The present invention relates to the field of organic hazardous waste treatment technology and equipment, and in particular to an organic hazardous waste integrated plasma multi-stage gasification melting furnace device and method, belonging to the technical field of organic hazardous waste disposal. Background Art

[0002] The comprehensive treatment of organic hazardous waste usually adopts rotary kiln incineration technology. When the rotary kiln is used for comprehensive incineration treatment of various types of organic hazardous waste, there are problems such as incomplete treatment, high thermal loss rate of incineration residue, small actual treatment volume, and dioxin pollution. The incineration residue and fly ash are still hazardous wastes and need to be further stabilized and solidified for landfill disposal, which will pose a risk of soil and groundwater pollution and hinder the large-scale, clean and resource-based development of rotary kiln incineration technology.

[0003] When fixed-bed pyrolysis and gasification is used to treat various types of organic hazardous wastes, the pyrolysis and gasification process is slow and the temperature is low due to the limitations of the thermochemical reaction kinetics of organic hazardous wastes. The pyrolysis and gasification process is incomplete and a large amount of solid semi-coke with a high carbon content will be produced, resulting in a residue thermal loss rate far exceeding 5%, which cannot meet the requirements of the hazardous waste incineration pollution control standards. At the same time, the pyrolysis and gasification reaction conditions of multi-component organic matter are different, and random chain breaking of organic matter will produce a large amount of tar, causing blockage of pyrolysis and gasification equipment and flue. Therefore, the fixed-bed pyrolysis and gasification technology has poor material universality and poor operational reliability.

[0004] Rotary oxygen-free pyrolysis furnaces usually use an external jacket indirect heating method to treat organic hazardous wastes. The heat from the external jacket heats the organic hazardous wastes through the rotary kiln cylinder by heat conduction and heat radiation. The rotary oxygen-free pyrolysis furnace has a small heat transfer area and low heat transfer efficiency, and the equipment is difficult to scale up. Limited by the temperature resistance of the rotary kiln body material, the pyrolysis temperature of the rotary oxygen-free pyrolysis furnace is low, the pyrolysis reaction conditions of multi-component organic matter are different, the organic matter is randomly broken, the components of the pyrolysis products are dispersed, the product quality is low, the product is difficult to control in a targeted manner, and the degree of resource utilization is low. Therefore, the rotary oxygen-free pyrolysis furnace has poor material adaptability and is only suitable for treating specific and single types of organic hazardous wastes.

[0005] At present, the comprehensive treatment of various types of organic hazardous wastes by rotary kiln incineration technology and fixed bed pyrolysis gasification technology lacks effective process control, which mainly includes pyrolysis, gasification and combustion stages. Different types and compositions of organic hazardous wastes have different pyrolysis characteristics. Different pyrolysis gaseous products and pyrolysis solid products, namely solid pyrolysis semi-coke, will be produced in the pyrolysis stage. The gasification and combustion of solid semi-coke requires high temperature and long time, and the reaction process is extremely slow. Therefore, the process control of thermochemical treatment directly determines the treatment efficiency, incineration removal rate and residue thermal burn reduction rate of rotary kiln incinerator and fixed bed pyrolysis gasification furnace. The pyrolysis and gasification combustion characteristics of organic hazardous wastes have a very important influence on the operating process parameters such as feed rate, air supply, auxiliary fuel amount, furnace temperature, furnace oxygen concentration, residence time, flue gas composition, flue gas volume, etc. The process control of traditional rotary kiln incinerator and fixed bed pyrolysis gasification furnace is not perfect, and further improvement is needed in terms of residue thermal burn reduction rate, incineration removal rate and dioxin pollution control.

[0006] At present, there are certain defects and deficiencies in the application of rotary kiln incinerators, fixed-bed pyrolysis gasification furnaces and rotary oxygen-free pyrolysis furnaces in the comprehensive treatment of organic hazardous wastes. Although the rotary kiln incinerator has strong material universality, it has problems such as high thermal burn-off rate of residues, small actual treatment volume, and dioxin pollution; although the fixed-bed pyrolysis gasification furnace has low investment and operation costs, it has poor material universality, slow treatment process, high thermal burn-off rate of residues, and large secondary pollution; although the rotary oxygen-free pyrolysis furnace has a high degree of resource utilization, the pyrolysis products can only be used as primary alternative fuels or raw materials, and the product value is low. At the same time, there are also problems such as poor material universality, low thermal efficiency, and difficulty in equipment expansion. Therefore, it is urgent to solve the application balance problem of comprehensive treatment technology for organic hazardous wastes in terms of material universality, process control, treatment capacity, reduction of secondary hazardous wastes, reduction of gas pollutants, and resource utilization.

[0007] At present, the demonstration applications of plasma methods for treating various types of organic hazardous wastes in China mainly include plasma pyrolysis furnace, fixed-bed plasma gasification and melting integrated furnace, pyrolysis furnace coordinated with plasma melting furnace and other technologies.

[0008] Plasma pyrolysis technology uses a cylindrical vertical furnace with a plasma torch located on the top of the furnace body. The plasma jet acts vertically downward on organic matter, which decomposes under the bombardment of plasma and melts inorganic ash at high temperature to form glassy slag. At present, the reaction mechanism of plasma pyrolysis technology is still unclear, and the reaction process is difficult to effectively control. Only a small part of the plasma participates in the pyrolysis reaction, and most of the plasma is converted into flue gas waste heat by thermal radiation. Therefore, the thermal efficiency of plasma pyrolysis technology is low, the processing efficiency is low, and the energy consumption is high.

[0009] The fixed-bed plasma gasification and melting integrated furnace is affected by the differences in the pyrolysis characteristics of organic matter with different components. The slow pyrolysis process will affect the rapid progress of the subsequent gasification process, so its material universality is poor.

[0010] The technology of pyrolysis furnace coordinated with plasma melting furnace means that the pyrolysis furnace and the plasma melting furnace share a flue gas purification system. Various types of organic hazardous wastes are first treated by the pyrolysis furnace, and then the plasma melting furnace coordinates the treatment of the pyrolysis residues produced by the pyrolysis furnace, thereby achieving vitrification treatment of various types of organic hazardous wastes. Pyrolysis furnaces often use fixed beds, rotary oxygen-free pyrolysis furnaces, fluidized beds and other technologies. These pyrolysis technologies have poor material universality, low treatment efficiency, difficult reaction process control, incomplete treatment, and secondary pollution problems have not been effectively solved. The plasma melting process of the pyrolysis residues has high energy consumption. Therefore, the cleanliness, resource utilization, and large-scale level of the pyrolysis furnace coordinated with plasma melting furnace technology needs to be further improved. Summary of the invention

[0011] The technical problem to be solved by the present invention is to provide an integrated plasma multi-stage gasification and melting furnace device and method for organic hazardous waste, improve the material universality of thermochemical treatment of various types of organic hazardous wastes, strengthen the regulation of thermochemical treatment process, improve the treatment efficiency and waste-to-energy efficiency of the thermochemical treatment process, and simultaneously realize ash self-melting during the thermochemical treatment of various types of organic hazardous wastes, thereby realizing the large-scale, resource-based and clean development of thermochemical treatment technology.

[0012] To achieve the above-mentioned objectives, the present invention adopts the following technical scheme: an integrated plasma multi-stage gasification and melting furnace device for organic hazardous waste, comprising a countercurrent rotary primary gasification furnace, a vertical secondary gasification furnace, a molten pool, an organic hazardous waste spiral feeding device, a flux feeding device, a burner, a plasma torch, a primary gasification blower, a secondary gasification blower, an oxygen meter and a synthesis gas component analyzer.

[0013] Furthermore, the countercurrent rotary primary gasifier comprises a horizontal rotary furnace body, a kiln tail hood, a kiln head hood, a synthesis gas outlet pipe, an emergency chimney, a kiln tail sealing system, a kiln head sealing system and a kiln head sight glass; the angle between the axial center line of the horizontal rotary furnace body and the horizontal line is 2 to 4°; the kiln tail sealing system and the kiln head sealing system are arranged at the connection between the horizontal rotary furnace body and the kiln tail hood and the kiln head hood, and together constitute a rotary primary gasifier sealing system, so that the air leakage of the primary gasifier is controlled within 2%; the emergency chimney and the synthesis gas outlet are centrally arranged on the kiln tail hood, and the synthesis gas outlet is connected to the secondary combustion chamber inlet through the synthesis gas outlet pipe; the kiln head sight glass is arranged on the kiln head hood panel and intersects with the axial center line of the horizontal rotary furnace body, so as to facilitate the observation of the gasification reaction process of organic hazardous waste in the primary gasifier, and is conducive to assisting the adjustment of the primary gasification process conditions and operating parameters.

[0014] Furthermore, the vertical secondary gasifier includes a vertical cylindrical furnace body and a sight glass; the top of the vertical cylindrical furnace body is connected to the bottom of the kiln head hood of the primary gasifier through a flange; the sight glass is arranged at the lower part of the vertical cylindrical furnace body, which is convenient for observing the high-temperature gasification and melting process of the solid semi-coke plasma in the secondary gasifier, and is beneficial to assist in adjusting the secondary gasification and melting process conditions and operating parameters.

[0015] Furthermore, the molten pool includes a flat cylindrical body and a slag outlet; the top of the flat cylindrical body is connected to the bottom of the secondary gasification furnace through a flange.

[0016] Furthermore, the organic hazardous waste spiral feeding device is connected to the kiln tail hood of the countercurrent rotary primary gasifier; the flux feeding device is connected to the kiln head hood of the countercurrent rotary primary gasifier; the burner is arranged in the middle of the kiln head hood panel of the countercurrent rotary primary gasifier; the plasma torch is located at the lower part of the vertical secondary gasifier cylinder; the primary gasification fan is connected to the circular kiln head hood of the countercurrent rotary primary gasifier through an air duct, and the primary gasification wind enters the primary gasification furnace tangentially to increase the air turbulence in the primary gasification furnace; the secondary gasification fan is connected to the lower part of the vertical secondary gasifier through an annular air duct; the oxygen meter is located in the horizontal section of the syngas outlet pipeline of the countercurrent rotary primary gasifier; the syngas component analyzer is located in the horizontal section of the syngas outlet pipeline of the countercurrent rotary primary gasifier.

[0017] Furthermore, the counter-current rotary primary gasifier is provided with a first temperature sensor and a second temperature sensor at the kiln tail hood and the kiln head hood, respectively; and a third temperature sensor is provided at the lower part of the vertical secondary gasifier.

[0018] Furthermore, the counter-current rotary primary gasifier is provided with a first pressure sensor and a second pressure sensor at the kiln tail hood and the kiln head hood, respectively; and a third pressure sensor is provided at the lower part of the vertical secondary gasifier.

[0019] Furthermore, the primary gasification fan and the secondary gasification fan are both frequency-controlled to automatically adjust the primary gasification air volume and the secondary gasification air volume, thereby realizing the oxygen content control of the organic hazardous waste integrated plasma multi-stage gasification melting furnace device.

[0020] Furthermore, the burner adopts a split structure, and the burner power and the first temperature sensor form a control loop to automatically adjust the burner auxiliary fuel flow and the burner fan combustion air flow to achieve the device start-up and shutdown furnace temperature control and the first-stage gasification furnace gasification temperature control during normal operation.

[0021] An organic hazardous waste integrated plasma multi-stage gasification and melting furnace device, characterized in that: it comprises an organic hazardous waste integrated plasma multi-stage gasification and melting furnace device, and also 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, and a sewage treatment system. The discharge port of the pretreatment system is connected to the feed port of the spiral feed device of the organic hazardous waste integrated plasma multi-stage gasification and melting furnace device, and the synthesis gas outlet of the organic hazardous waste integrated plasma multi-stage gasification and melting furnace device is connected to the synthesis gas outlet of the secondary combustion chamber. The flue gas inlet is connected, the flue gas outlet of the secondary combustion chamber is connected to the flue gas inlet of the waste heat recovery device, the flue gas outlet of the waste heat recovery device is connected to the flue gas inlet of the flue gas purification device, the flue gas outlet of the flue gas purification device is connected to the flue gas inlet of the induced draft fan, and the flue gas outlet of the induced draft fan is connected to the chimney inlet, so as to achieve emission of waste gas in compliance with the standards; the fly ash generated by the waste heat recovery device and the flue gas purification device is collected and granulated for pre-treatment, and then returned to the vertical secondary gasification furnace by the flux feeding device for melting and disposal, and the production waste water generated by the waste heat recovery device and the flue gas purification device is pumped to the sewage treatment system for treatment.

[0022] Furthermore, the flue gas purification device comprises an SNCR denitrification device, a quenching device, a dry deacidification device, an activated carbon injection device, a bag dust removal device, a precooling tower, a two-stage wet deacidification tower, a wet electrostatic precipitator, a GGH flue gas heat exchanger, an SGH flue gas reheater, and an SCR denitrification device, which are arranged in the high temperature section of the flue gas of the waste heat recovery device at 850-1100°C; the flue gas outlet of the quenching device and the material outlet of the activated carbon injection device are connected to the flue gas inlet of the dry deacidification device, the flue gas outlet of the dry deacidification device is connected to the flue gas inlet of the bag dust removal device, the flue gas outlet of the bag dust removal device is connected to the flue gas inlet of the precooling tower, and the flue gas outlet of the precooling tower is connected to the flue gas inlet of the first-stage wet deacidification tower. The flue gas outlet of the first-level wet deacidification tower is connected to the flue gas inlet of the second-level wet deacidification tower, the flue gas outlet of the second-level wet deacidification tower is connected to the flue gas inlet of the wet electrostatic precipitator, the flue gas outlet of the wet electrostatic precipitator is connected to the original flue gas inlet of the GGH flue gas heat exchanger, the original flue gas outlet of the GGH flue gas heat exchanger is connected to the flue gas inlet of the SGH flue gas reheater, the flue gas outlet of the SGH flue gas reheater is connected to the flue gas inlet of the SCR denitrification device, the flue gas outlet of the SCR denitrification device is connected to 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 to the flue gas inlet of the induced draft fan, the flue gas is pressurized by the induced draft fan and discharged into the atmosphere through the chimney, so as to achieve standard emission of waste gas.

[0023] An integrated plasma multi-stage gasification and melting furnace method for organic hazardous waste, characterized by comprising the following steps:

[0024] Step 1: Organic hazardous waste is transported through the kiln tail hood into the countercurrent rotary primary gasifier by a spiral feeding device, and the organic hazardous waste and the combustion-supporting air in the furnace are in a state of opposite motion; the hazardous waste spiral feeding device adopts frequency conversion control to adjust the feeding rate; according to the temperature measurement value of the first temperature sensor, the burner power is automatically adjusted to control the gasification temperature of the primary gasifier; the primary gasification fan adopts frequency conversion control to adjust the primary gasification air volume to ensure that the primary gasifier forms an obvious oxygen concentration gradient along the axial direction, thereby realizing the oxygen content control of the organic hazardous waste integrated plasma multi-stage gasification melting furnace device; the countercurrent rotary primary gasifier rotary drive system adopts frequency conversion control to automatically adjust the waste residence time in the primary gasifier, thereby controlling the gasification reaction time of the primary gasifier; multi-type and complex component organic hazardous waste During comprehensive gasification, by balancing and adjusting the feed rate, primary gasification air volume, auxiliary fuel amount, gasification temperature ~ 1000℃, gasification reaction time, synthesis gas oxygen content 0.2% ~ 1%, synthesis gas CO concentration 7% ~ 12%, synthesis gas CH4 concentration less than 1%, the organic hazardous waste undergoes drying, rapid pyrolysis, and rapid gasification stages in the primary gasifier, and the high-boiling point, difficult-to-decompose organic matter is completely converted into H2, CO and CH4 synthesis gas, fundamentally solving the problem of slow processing process of traditional pyrolysis gasification technology; the synthesis gas enters the secondary combustion chamber for gaseous homogeneous combustion, the reliability and stability of the secondary combustion chamber operation are significantly enhanced, and the waste heat recovery efficiency of the waste heat recovery device is greatly improved; the solid semi-coke produced by the primary gasifier falls into the vertical secondary gasifier as the primary gasifier rotates, so that the solid semi-coke is further processed;

[0025] Step 2: Solid semi-coke forms a material bed layer of a certain height in the vertical secondary gasifier, and flux and coke are added to the vertical secondary gasifier through the flux feeding device. The difference in specific gravity of coke causes it to gather between the material bed layer and the molten slurry to form a coke bed layer. The coke bed layer provides support for the material bed layer and guides the plasma jet into the material bed layer. The coke bed layer provides a pore channel for the downward flow of slag and metal; the high temperature and high reaction activity of the plasma make the fixed carbon in the solid semi-coke quickly gasify into CO, so that the ash in the solid semi-coke is self-melted during the high-temperature rapid gasification process of the plasma; the high-temperature synthesis gas generated by the vertical secondary gasifier is used as a partial heat source of the countercurrent rotary primary gasifier, which can significantly accelerate the primary gasification reaction process; according to the temperature measurement value of the second temperature sensor, the plasma torch power and the secondary gasification air volume are automatically adjusted , thereby controlling the secondary gasification temperature and realizing rapid gasification of fixed carbon, solving the problems of slow reaction process and incomplete reaction of solid semi-coke in traditional thermochemical treatment technology; at the same time, by adjusting the type and amount of flux, the ash melting point temperature of ash content can be effectively reduced to improve the fluidity of slurry, thereby reducing the energy consumption of the system; when the slurry in the molten pool reaches a certain material level, the slag is discharged out of the furnace through the slag outlet of the molten pool at the bottom of the secondary gasifier, and after water quenching and cooling, a glassy substance is formed, which is used as a general solid waste for resource utilization, avoiding the generation of secondary hazardous waste; through steps one and two, hierarchical gasification and segmented control of organic hazardous waste are realized, the process adjustment and control of the whole gasification process are strengthened, the material adaptability and gasification efficiency of the device and system are significantly improved, the prerequisite for dioxin synthesis is eliminated, and the dioxin pollution problem is solved from the source;

[0026] Step 3: Synthesis gas is burned in the secondary combustion chamber in a highly efficient homogeneous manner, and a large amount of heat can be released without the need to add auxiliary fuel, thereby maintaining the operating temperature of the secondary combustion chamber ≥ 1100°C; the high-temperature flue gas from the secondary combustion chamber enters the waste heat recovery device for recovery and power generation or direct steam utilization, which can improve the economic efficiency of the system operation; before the country releases special technical specifications and pollution control standards for the treatment of hazardous wastes with plasma technology, the 500°C flue gas after waste heat recovery needs to enter the quenching device and be rapidly cooled to less than 200°C within 1 second to avoid the temperature range of dioxin resynthesis;

[0027] Step 4: The flue gas rapidly cooled by the quenching device enters the dry deacidification device to remove part of the acid gases such as SO2, HCl and HF. The flue gas after dry deacidification is adsorbed by activated carbon to remove heavy metals and dioxins, and then filtered by a bag dust removal device to remove most of the particulate matter. The flue gas after dust removal is further removed by a precooling tower and a two-stage wet deacidification tower to remove acid gases such as SO2, HCl and HF. The flue gas after wet deacidification is further removed by a wet electrostatic precipitator to remove particulate matter, acid mist and salt mist;

[0028] Step 5: The 68°C flue gas at the outlet of the wet electrostatic precipitator is heated to 140°C through the GGH flue gas heat exchanger; the flue gas outlet of the wet electrostatic precipitator is connected to the original flue gas inlet of the GGH flue gas heat exchanger, and the flue gas outlet of the SCR denitrification device is connected to the clean flue gas inlet of the GGH flue gas heat exchanger. After the high-temperature flue gas and the low-temperature flue gas are heat exchanged, the flue gas temperature at the original flue gas outlet of the GGH flue gas heat exchanger rises to about 140°C, and the flue gas temperature at the clean flue gas outlet of the GGH flue gas heat exchanger drops from 200°C to 130°C, thereby achieving the purpose of recovering the waste heat of the SCR denitrification flue gas and reducing the energy consumption of the system;

[0029] Step 6: The flue gas heated by GGH is further heated to ≥200℃ by SGH flue gas reheater. SGH flue gas reheater uses 300℃ superheated steam generated by waste heat recovery device to heat the flue gas to meet the working temperature requirements of SCR denitrification device; the outlet flue gas of SGH flue gas reheater enters SCR catalytic denitrification device for further deep removal of NO X ;

[0030] Step 7: The clean flue gas outlet of the GGH flue gas heat exchanger is connected to the induced draft fan inlet, and the clean flue gas is pressurized by the induced draft fan and discharged into the atmosphere through the chimney.

[0031] Compared with the existing rotary kiln incinerator, fixed bed pyrolysis gasification furnace, plasma pyrolysis furnace, fixed bed plasma gasification and melting integrated furnace, pyrolysis furnace coordinated with plasma melting furnace, the present invention has the following remarkable effects: the countercurrent rotary primary gasification furnace performs high-temperature pyrolysis and gasification on organic hazardous waste, the vertical secondary gasification furnace performs plasma high-temperature gasification on solid semi-coke, the integrated application of the countercurrent rotary primary gasification furnace and the vertical secondary gasification furnace realizes graded gasification and segmented control of organic hazardous waste, strengthens the regulation of pyrolysis and gasification of organic matter and gasification process of solid semi-coke, the high temperature and high reaction activity of plasma accelerates the gasification process of solid semi-coke, the fixed carbon gasification is more thorough, and the fixed carbon high-temperature gasification simultaneously realizes ash self-melting Vitrification eliminates the technical limitation of plasma being only a high-temperature heat source, greatly reducing the energy consumption of the device and system; it solves the problems of difficult reaction process control, slow treatment process, and incomplete treatment in existing rotary kiln incinerators, fixed-bed pyrolysis gasification furnaces, plasma pyrolysis furnaces, and fixed-bed plasma gasification and melting integrated furnaces, and significantly accelerates the thermochemical treatment process of various types of complex component hazardous wastes, making the thermochemical treatment more thorough, the gasification efficiency higher, and the waste-to-energy efficiency higher. Therefore, the material adaptability, process reliability, and operating economy of the integrated plasma multi-stage gasification and melting technology for organic hazardous waste are significantly better than those of the existing technology, truly realizing the harmless, reduced, and resource-based treatment of various types and multi-component organic hazardous wastes. BRIEF DESCRIPTION OF THE DRAWINGS

[0032] Figure 1 It is a schematic diagram of an integrated plasma multi-stage gasification and melting furnace device for organic hazardous waste according to the present invention.

[0033] Figure 2 This is a schematic diagram of the kiln tail side of an integrated plasma multi-stage gasification and melting furnace device for organic hazardous waste according to the present invention.

[0034] Figure 3 This is a schematic diagram of the kiln head side of an integrated plasma multi-stage gasification and melting furnace device for organic hazardous waste according to the present invention.

[0035] Figure 4 This is a schematic AA cross-sectional view of an integrated plasma multi-stage gasification and melting furnace device for organic hazardous waste according to the present invention.

[0036] Figure 5 It is a schematic diagram of an organic hazardous waste integrated plasma multi-stage gasification and melting furnace system of the present invention.

[0037] In the figure: 1-countercurrent rotary primary gasifier, 2-vertical secondary gasifier, 3-molten pool; 4-horizontal rotary furnace body, 5-corundum mullite refractory brick, 6-kiln tail cover, 7-kiln head cover, 8-synthesis 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 wind inlet pipe, 12-burner, 121-burner interface, 13-burner fan, 14 -kiln tail sealing system, 15-kiln head sealing system, 16-oxygen meter, 17-synthesis gas component analyzer, 18-kiln head sight glass; 19-vertical cylindrical furnace body, 20-chrome corundum refractory brick, 21-plasma torch, 22-flux feeding device, 221-flux feeding port, 23-secondary gasification fan, 231-secondary gasification annular air duct, 24-flange, 25-sight glass; 26-chrome zirconium corundum refractory brick, 27-flat cylinder, 28-slag outlet, 29-flange. DETAILED DESCRIPTION

[0038] In order to elaborate on the technical scheme adopted by the present invention to achieve the predetermined technical purpose, the technical scheme in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only partial embodiments of the present invention, rather than all embodiments, and the technical means or technical features in the embodiments of the present invention can be replaced without paying creative work. The present invention will be described in detail below with reference to the drawings and in conjunction with the embodiments.

[0039] like Figure 1 , Figure 2 , Figure 3 , Figure 4As shown, an integrated plasma multi-stage gasification and melting furnace device for organic hazardous waste of the present invention includes a countercurrent rotary primary gasification furnace 1, a vertical secondary gasification furnace 2, a molten pool 3, an organic hazardous waste spiral feeding device 10, a flux feeding device 22, a burner 12, a plasma torch 21, a primary gasification fan 11, a secondary gasification fan 23, an oxygen meter 16 and a synthesis gas component analyzer 17.The countercurrent rotary primary gasifier 1 is connected to the vertical secondary gasifier 2 through the kiln head cover 7, and the vertical secondary gasifier 2 is connected to the molten pool 3. The connection between the kiln head cover 7 and the vertical secondary gasifier 2 and the connection between the vertical secondary gasifier 2 and the molten pool 3 are respectively connected by flanges 24 and 29, which is convenient for the maintenance and overhaul of the refractory materials of the device; the organic hazardous waste spiral feeding device 10 is connected to the kiln tail cover 6 of the countercurrent rotary primary gasifier 1, and the organic hazardous waste is transported through the spiral feeding device 10 and the amount of organic hazardous waste added per unit time is controlled. The organic hazardous waste enters the countercurrent rotary primary gasifier 1 and moves in the opposite direction with the combustion-supporting wind. The heat and mass transfer effect in the furnace is good, and the organic hazardous waste undergoes drying, rapid pyrolysis, rapid Rapid gasification stage; the burner 12 is arranged in the middle of the kiln head cover 7 panel of the countercurrent rotary primary gasifier 1, and adopts a split structure. The burner 12 and the first temperature sensor form a control loop to automatically adjust the auxiliary fuel flow rate and the burner fan 13 combustion air flow rate, which are used for the device to start and stop the furnace temperature control and the gasification temperature adjustment of the primary gasifier during normal operation; the primary gasification fan 11 is connected to the kiln head cover 7 of the countercurrent rotary primary gasifier 1 through the primary gasification tangential wind inlet pipe 111, and the primary gasification wind enters the primary gasifier 1 tangentially to increase the air turbulence. The primary gasification fan 11 is controlled by frequency conversion to automatically adjust the primary gasification air volume to realize the oxygen content control of the device oxygen meter 16; the plasma torch 21 is located at the vertical second At the lower part of the cylinder of the first-stage gasifier 2, a plasma torch 21 is equipped with a power supply, circulating cooling water and instrument gas. The plasma torch 21 and the second temperature sensor form a control loop to automatically adjust the operating power of the plasma torch, accelerate the gasification process of the solid semi-coke, and improve the gasification efficiency of the solid semi-coke; the second-stage gasification fan 23 is connected to the lower part of the vertical second-stage gasifier 2 through the second-stage gasification annular air duct 231, and the second-stage gasification air volume is automatically adjusted through the frequency conversion control of the second-stage gasification fan 23 to realize the auxiliary control of the oxygen content of the device oxygen meter 16; the flux feeding device 22 is connected to the kiln head cover 7 of the countercurrent rotary first-stage gasifier 1, and the flux is transported into the vertical second-stage gasifier 2 through the feeding device 22. By adjusting the type and amount of the flux, the control The ash melting slag type is produced to reduce the ash melting point temperature and realize the energy consumption control of the device operation; the oxygen meter 16 is located in the horizontal section of the synthesis gas outlet pipeline 8 of the countercurrent rotary primary gasifier 1, monitors the oxygen content of the synthesis gas at 0.2% to 1%, adjusts the air supply volume and air supply ratio of the primary gasification fan 11 and the secondary gasification fan 23, and ensures that the device is in an efficient gasification operation state; the synthesis gas component analyzer 17 is located in the horizontal section of the synthesis gas outlet pipeline 8 of the countercurrent rotary primary gasifier 1, automatically monitors the calorific value of the synthesis gas and the content of CO, H2, and CH4, so as to balance and adjust the process conditions and operating parameters of the device, control the CO concentration at 7% to 12%, and the CH4 concentration within 1%, to ensure that the device is in a safe and reliable operation state.

[0040] The countercurrent rotary primary gasification furnace 1 comprises a horizontal rotary furnace body 4, a refractory material 5, a kiln tail hood 6, a kiln head hood 7, a synthesis gas outlet pipe 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 angle between the axial center line of the horizontal rotary furnace body 4 and the horizontal line is 2 to 4 degrees; the lining refractory material 5 of the countercurrent rotary primary gasification furnace 1 adopts corundum mullite refractory bricks; a kiln is arranged at the connection between the horizontal rotary furnace body 4 and the kiln tail hood 6 and the kiln head hood 7. The tail sealing system 14 and the kiln head sealing system 15 constitute a double sealing system of the primary gasifier 1, which controls the air leakage of the countercurrent rotary primary gasifier 1 within 2%; the synthesis gas outlet pipeline 8 and the emergency chimney 9 are centrally arranged on the kiln tail cover 6; the kiln head sight glass 18 is arranged on the kiln head cover panel, intersecting with the axial center line of the horizontal rotary furnace body 4, so as to facilitate the observation of the gasification process of organic hazardous waste in the primary gasifier 1, and is conducive to assisting the adjustment of the primary gasification process conditions and operating parameters.

[0041] The vertical secondary gasifier 2 includes a vertical cylindrical furnace body 19, a refractory material 20 and a sight glass 25; the top of the vertical cylindrical furnace body 19 is connected to the bottom of the kiln head cover 7 of the countercurrent rotary primary gasifier 1 through a flange 24; the lining refractory material 20 of the vertical secondary gasifier 2 adopts chrome corundum refractory bricks; the sight glass 25 is arranged at the lower part of the vertical cylindrical furnace body 19, which is convenient for observing the secondary gasification process and ash melting process of the solid semi-coke in the vertical secondary gasifier 2, and is beneficial to assist in adjusting the secondary gasification melting process conditions and operating parameters.

[0042] The molten pool 3 includes a flat cylindrical body 27, a refractory material 26 and a slag outlet 28; the top of the flat cylindrical body 27 is connected to the bottom of the vertical secondary gasifier 2 through a flange 29; the refractory material 26 lined in the molten pool 3 adopts chromium-zirconium-corundum refractory bricks that are resistant to erosion by molten slag.

[0043] The kiln tail hood 6 and the kiln head hood 7 of the counter-current rotary primary gasifier 1 are respectively provided with a first temperature sensor and a second temperature sensor, and a third temperature sensor is provided at the lower part of the vertical secondary gasifier 2. The first temperature sensor is used to monitor the gasification temperature of the counter-current rotary primary gasifier 1 and adjust the operating power of the burner 12, thereby controlling the primary gasification temperature of the counter-current rotary primary gasifier 1; the second temperature sensor is used to monitor the gasification temperature of the vertical secondary gasifier 2 and adjust the operating power of the plasma torch 21, thereby controlling the secondary gasification temperature of the vertical secondary gasifier 2; the combined application of the second temperature sensor and the first temperature sensor is helpful for real-time monitoring and analysis of fluctuations in operating parameters caused by changes in the composition of organic hazardous waste and pyrolysis and gasification characteristics, and is convenient for timely optimization and adjustment of gasification process conditions and operating parameters; the third temperature sensor is used to monitor the ash melting temperature of the vertical secondary gasifier 2, so as to timely adjust the type and dosage of flux and improve the fluidity of slag.

[0044] The kiln tail hood 6 and the kiln head hood 7 of the counter-current rotary primary gasifier 1 are respectively provided with a first pressure sensor and a second pressure sensor, and a third pressure sensor is provided at the lower part of the vertical secondary gasifier 2. The first pressure sensor is used to monitor the negative pressure at the kiln tail of the counter-current rotary primary gasifier 1, the second pressure sensor is used to monitor the negative pressure at the kiln head of the counter-current rotary primary gasifier 1, and the third pressure sensor is used to monitor the negative pressure at the vertical secondary gasifier 1. According to the change of the negative pressure of the device, the air volume and air pressure of the induced draft fan are automatically adjusted to ensure that the device operates in a negative pressure closed state; if the device has a positive pressure, the emergency chimney is automatically opened to ensure that the system operates in a safe state.

[0045] like Figure 5 As shown, an organic hazardous waste integrated plasma multi-stage gasification and melting furnace system comprises an organic hazardous waste pretreatment system, an integrated plasma multi-stage gasification and 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, etc. The discharge port of the pretreatment system is connected to the feed port of the spiral feed device of the organic hazardous waste integrated plasma multi-stage gasification and melting furnace device, and the synthesis gas outlet pipeline of the organic hazardous waste integrated plasma multi-stage gasification and melting furnace device is connected to the synthesis gas inlet of the secondary combustion chamber. The flue gas outlet of the secondary combustion chamber is connected to the flue gas inlet of the waste heat recovery device, the flue gas outlet of the waste heat recovery device is connected to the flue gas inlet of the flue gas purification device, the flue gas outlet of the flue gas purification device is connected to the flue gas inlet of the induced draft fan, and the flue gas outlet of the induced draft fan is connected to the chimney inlet to achieve standard emission of waste gas; the fly ash generated by the waste heat recovery device and the flue gas purification device is collected and granulated for pre-treatment, and then returned to the vertical secondary gasification furnace for melting and disposal by the flux feeding device, and the waste water generated by the waste heat recovery device and the flue gas purification device is pumped to the sewage treatment system for treatment. Organic hazardous waste is subjected to plasma multi-stage gasification and melting treatment to produce synthesis gas and glassy slag. The glassy slag can be used as general building materials or for high-value utilization. The synthesis gas enters the secondary combustion chamber for efficient combustion. The 1100℃ high-temperature flue gas in the secondary combustion chamber enters the membrane wall boiler waste heat recovery device. The flue gas is cooled to 500℃ after waste heat recovery. The flue gas at the outlet of the waste heat recovery device enters the quenching device to be cooled to 200℃, thereby avoiding the temperature range for the resynthesis of dioxins in the flue gas.

[0046] The flue gas purification device includes a SNCR denitrification device, a quenching device, a dry deacidification device, an activated carbon injection device, a bag dust removal device, a precooling tower, a two-stage wet deacidification tower, a wet electrostatic precipitator, a GGH flue gas heat exchanger, an SGH flue gas reheater, and an SCR denitrification device. The high-temperature section of the flue gas of the waste heat recovery device is equipped with an SNCR denitrification device, which uses a dual-fluid spray gun to meter and spray 10% urea solution to reduce NO in the flue gas. XThe flue gas outlet of the waste heat recovery device is connected to the flue gas inlet of the quenching device. The quenching water is pumped to the double-fluid spray gun on the top of the quenching tower. The quenching water is atomized into 40μm small particle mist water by compressed air and then sprayed into the quenching tower. The quenching water and the flue gas are fully in contact and heat exchange. The flue gas is quickly cooled to 200℃ within 1 second, avoiding the temperature range of 500℃~200℃ for the resynthesis of dioxins in the flue gas; the flue gas outlet of the quenching device and the activated carbon outlet of the activated carbon injection device are connected to the flue gas inlet of the dry deacidification device. The dry deacidification device is equipped with a Venturi tube mixer. The slaked lime and activated carbon are mixed. After being fully mixed with the flue gas by the Venturi tube mixer, part of the acidic gases such as HCl, SO2, HF in the flue gas is removed by neutralization reaction with slaked lime. The acidic gas removal rate of the dry deacidification device is not less than 20%. The activated carbon adsorption removes dioxins and some volatile heavy metals in the flue gas; the flue gas outlet of the dry deacidification device is connected to the flue gas inlet of the bag dust removal device, and the particulate matter in the flue gas is filtered and removed by the bag dust removal device. Most heavy metals, such as lead, exist in solid form below 300°C, condense with the particulate matter and are filtered and removed by the bag dust removal device. After the bag dust removal, the concentration of particulate matter in the flue gas is less than 10mg / m 3The flue gas outlet of the bag dust removal device is connected to the flue gas inlet of the precooling tower. A precooling water spray gun is arranged on the upper part of the precooling tower. The precooling spray water contacts and exchanges heat with the flue gas downstream, and the flue gas temperature drops to 71°C, achieving the purpose of cooling and humidifying the flue gas. The flue gas outlet of the precooling tower is connected to the flue gas inlet of the primary wet deacidification tower. The flue gas contacts and reacts with the circulating alkali solution of the primary wet deacidification tower in countercurrent and a neutralization reaction occurs, so that most of the acid gases in the flue gas can be removed. The flue gas outlet of the primary wet deacidification tower is connected to the flue gas inlet of the secondary wet deacidification tower. The residual acid gases in the flue gas continue to contact with the secondary wet deacidification tower. The circulating alkali solution contacts in countercurrent and reacts with neutralization, so that the acidic gas can be completely removed, and the wet deacidification efficiency can reach 99%; volatile heavy metals with high saturated vapor pressure such as mercury exist in the flue gas in gaseous form, and mercury reacts with HCl in the flue gas to be converted into HgCl2, which is a water-soluble compound. During the wet deacidification process, HgCl2 reacts with the circulating alkali solution and is removed; the flue gas outlet of the secondary wet deacidification tower is connected to the flue gas inlet of the wet electrostatic precipitator, which has a certain dust removal capacity and can cooperate with the bag filter to achieve flue gas particle removal. Ultra-low emission of particulate matter, and can effectively remove salt mist and acid mist in the flue gas, avoiding poisoning and deactivation of the SCR denitrification catalyst; in order to meet the SCR denitrification temperature requirement of 200℃, the GGH flue gas heat exchanger is first used to heat the flue gas at the outlet of the wet electrostatic precipitator. The flue gas outlet of the wet electrostatic precipitator is connected to the original flue gas inlet of the GGH flue gas heat exchanger, and the flue gas outlet of the SCR denitrification device is connected to the clean flue gas inlet of the GGH flue gas heat exchanger. After the 200℃ high-temperature flue gas at the SCR denitrification outlet is heat-exchanged with the 68℃ low-temperature flue gas at the wet electrostatic precipitator outlet, the original flue gas The temperature is raised to 140℃, and the clean flue gas is cooled to 130℃, realizing the waste heat utilization and system energy saving of the flue gas after SCR denitration. In order to meet the temperature requirements of SCR denitration, the SGH flue gas reheater is used to heat the flue gas for the second time. The SGH flue gas reheater uses the 300℃ superheated steam generated by the waste heat recovery device to heat the 140℃ flue gas at the original flue gas outlet of the GGH flue gas heat exchanger to 200℃. The flue gas outlet of the SGH flue gas reheater is connected to the flue gas inlet of the SCR denitration device. Under the action of the catalyst of the SCR denitration device, NO in the flue gas is X It undergoes a redox reaction with NH3 to convert NO X Catalytic reduction to N2, achieving NO XEmissions meet standards; the outlet flue gas temperature of the SCR denitrification device is 200℃. The high-temperature flue gas has high requirements on the temperature and corrosion resistance of the induced draft fan and chimney, which will directly increase the equipment investment and waste the flue gas waste heat. Therefore, the GGH flue gas heat exchanger is used to recover the flue gas waste heat after SCR denitrification. The flue gas outlet of the SCR denitrification device is connected to the clean flue gas inlet of the GGH flue gas heat exchanger. After the high-temperature clean flue gas of the GGH flue gas heat exchanger and the low-temperature original flue gas are heat exchanged, the low-temperature original flue gas from the wet electrostatic precipitator is heated, and the high-temperature clean flue gas from the SCR denitrification device is cooled; finally, the clean flue gas outlet of the GGH flue gas heat exchanger is connected to the induced draft fan inlet, and the flue gas is pressurized by the induced draft fan and discharged into the atmosphere through the chimney.

[0047] An integrated plasma multi-stage gasification and melting furnace method for organic hazardous waste, characterized by comprising the following steps:

[0048] Step 1: If Figure 1 , Figure 5As shown, the pre-treated organic hazardous waste is transported through the kiln tail hood 6 by the spiral feeding device 10 into the countercurrent rotary primary gasifier 1, and the organic hazardous waste and the combustion air in the furnace are in a state of opposite motion; the hazardous waste spiral feeding device 10 adopts a frequency converter to control and adjust the feeding rate; according to the temperature measurement value of the first temperature sensor of the kiln tail hood 6, the power of the burner 12 is automatically adjusted, that is, the auxiliary fuel flow rate and the combustion air flow rate of the burner fan 13 are automatically adjusted to realize the heating control of the plasma multi-stage gasification and melting device when the furnace is started and the cooling control of the furnace when the furnace is stopped, as well as the gasification temperature control of the primary gasifier 1 during normal operation; the primary gasification air volume is automatically adjusted through the frequency conversion control of the primary gasification fan 11, so as to realize the oxygen content control of the plasma multi-stage gasification and melting device oxygen meter 16 and the auxiliary control of the gasification temperature of the primary gasifier 1; by balancing and adjusting the power of the burner 12 and the primary gasification air volume of the primary gasification fan 11, the process balance between the gasification temperature and the oxygen content of the primary gasifier 1 is realized, which greatly enhances the material adaptability of the primary gasifier 1; The rotary drive system of furnace 1 is controlled by a frequency converter to automatically adjust the waste residence time of the first-stage gasification furnace 1 and control the gasification reaction time of hazardous waste; when multi-type and multi-component organic hazardous wastes are gasified, the running frequency (feeding rate) of the feed screw 10, the first-stage gasification air volume, the auxiliary fuel volume, the gasification temperature of 1000°C, the gasification reaction time, the oxygen content of the synthesis gas of 0.2% to 1%, the CO concentration of the synthesis gas of 7% to 12%, and the CH4 concentration of the synthesis gas of less than 1% are balanced and adjusted, so that the organic hazardous wastes are dried, In the rapid pyrolysis and rapid gasification stage, high-boiling-point, difficult-to-decompose organic matter is converted into combustible gases such as H2, CO and CH4 and solid semi-coke, which fundamentally solves the problem of slow reaction in the traditional pyrolysis and gasification process; the synthesis gas enters the secondary combustion chamber through the synthesis gas outlet pipe 8 of the kiln tail hood 6 for gaseous homogeneous combustion, which enhances the reliability and stability of the secondary combustion chamber operation and is conducive to the efficient recovery and utilization of waste heat; the solid semi-coke falls into the vertical secondary gasification furnace 2 as the countercurrent rotary primary gasification furnace 1 rotates, realizing further processing of the solid semi-coke;

[0049] Step 2: If Figure 1As shown, the solid semi-coke forms a material bed layer of a certain height in the vertical secondary gasifier 2, and the flux and coke enter the vertical secondary gasifier 2 through the flux feeding device 22. The difference in specific gravity of the coke causes it to gather between the material bed layer and the slurry to form a coke bed layer, and the coke bed layer provides support for the material bed layer and guides the plasma jet into the material bed layer. The coke bed layer provides a pore channel for the downward flow of slag and metal; according to the temperature measurement value of the second temperature sensor of the kiln head cover 7, the operating power of the plasma torch 21 and the secondary gasification air volume of the secondary gasification fan 23 are automatically adjusted, and the high temperature and high reaction activity of the plasma make the fixed carbon in the solid semi-coke quickly gasify into CO, and the ash in the solid semi-coke realizes self-melting in the high-temperature rapid gasification process of the plasma. The high-temperature synthesis gas generated by the vertical secondary gasifier 2 is used as a partial heat source of the countercurrent rotary primary gasifier 1, which can significantly accelerate the primary gasification process; the plasma accelerates the gasification process of the solid semi-coke, The gasification efficiency of solid semi-coke is significantly improved, and the problems of slow and incomplete treatment of solid semi-coke in traditional thermochemical treatment are solved; according to the melting point of organic hazardous waste ash and the fluidity of slag at the slag outlet 28 of the vertical secondary gasifier 2, a reasonable slag shape is designed, the type and amount of flux added are adjusted, the melting temperature of ash in solid semi-coke is reduced, and the fluidity of slag is increased, thereby reducing the melting temperature of the secondary gasifier 2 and realizing low-power operation of the plasma torch 21; when the slurry in the molten pool 3 reaches a certain material level, the slag is discharged out of the furnace through the slag outlet 3 at the bottom of the secondary gasifier 2, and is used as a general solid waste for resource utilization, avoiding the generation of secondary hazardous waste; through steps one and two, the hierarchical gasification and segmented control of organic hazardous waste are realized, the process adjustment and control of the whole gasification process are strengthened, the material adaptability and gasification efficiency of the device and system are significantly improved, the prerequisite for dioxin synthesis is eliminated, and the dioxin pollution problem is solved from the source;

[0050] Step 3: If Figure 5 As shown, the synthesis gas is efficiently homogeneously burned in the secondary combustion chamber, and a large amount of heat can be released without the need to add auxiliary fuel, thereby maintaining the operating temperature of the secondary combustion chamber ≥ 1100℃; the high-temperature flue gas in the secondary combustion chamber enters the waste heat recovery device for waste heat recovery power generation or direct steam utilization, which can improve the economic efficiency of the system operation; before the country releases special technical specifications and pollution control standards for plasma technology to treat hazardous wastes, the 500℃ flue gas after waste heat recovery needs to enter the quenching device to rapidly cool down to less than 200℃ within 1 second to avoid the temperature range of dioxin resynthesis;

[0051] Step 4: If Figure 5As shown, the flue gas after rapid cooling by the quenching device enters the dry deacidification device to remove part of the acid gases such as SO2, HCl and HF. The flue gas after dry deacidification is adsorbed by activated carbon to remove heavy metals and dioxins, and then filtered by a bag dust removal device to remove most of the particulate matter; the flue gas after dust removal is further deeply removed by a precooling tower and a two-stage wet deacidification tower to further remove acid gases such as SO2, HCl and HF. The flue gas after wet deacidification is further removed by a wet electrostatic precipitator to remove particulate matter, acid mist and salt mist; Step five: as Figure 5 As shown, the 68℃ flue gas at the flue gas outlet of the wet electrostatic precipitator is heated to 140℃ by the GGH flue gas heat exchanger; the flue gas outlet of the wet electrostatic precipitator is connected to the original flue gas inlet of the GGH flue gas heat exchanger, and the flue gas outlet of the SCR denitrification device is connected to the clean flue gas inlet of the GGH flue gas heat exchanger. After the high-temperature flue gas and the low-temperature flue gas are heat exchanged, the flue gas temperature at the original flue gas outlet of the GGH flue gas heat exchanger rises to 140℃, and the flue gas temperature at the clean flue gas outlet of the GGH flue gas heat exchanger drops to 130℃, so as to achieve the purpose of recovering the waste heat of the SCR denitrification flue gas and reducing the energy consumption of the system;

[0052] Step 6: If Figure 5 As shown in the figure, the flue gas heated by GGH is further heated to 200℃ by SGH flue gas reheater. SGH flue gas reheater uses 300℃ superheated steam generated by waste heat recovery device to heat the flue gas to 200℃ to meet the working temperature requirements of SCR denitrification device; the flue gas heated by SGH enters SCR catalytic denitrification device for further deep removal of NO X ;

[0053] Step 7: If Figure 5 As shown, the clean flue gas at the outlet of the GGH flue gas heat exchanger is pressurized by the induced draft fan and then discharged into the atmosphere through the chimney.

[0054] The invention discloses an organic hazardous waste integrated plasma multi-stage gasification melting furnace device and method, comprising a countercurrent rotary primary gasifier, a vertical secondary gasifier, a molten pool, a hazardous waste spiral feeding device, a flux feeding device, a burner, a plasma torch, a primary gasification blower, a secondary gasification blower, an oxygen meter and a synthesis gas component analyzer; the countercurrent rotary primary gasifier comprises a horizontal rotating furnace body, a kiln tail cover, a kiln head cover, a synthesis gas outlet pipeline, an emergency chimney, a kiln tail sealing system, a kiln head sealing system and a sight glass; the vertical secondary gasifier comprises a vertical cylindrical furnace body and a sight glass; the molten pool comprises a flat cylindrical body and a slag outlet; wherein the hazardous waste spiral feeding device is connected to the countercurrent rotary primary gasifier kiln tail cover, the flux feeding device is connected to the countercurrent rotary primary gasifier kiln head cover, and the burner is arranged in the countercurrent rotary primary gasifier kiln In the middle of the hood panel, the plasma torch is located at the lower part of the vertical secondary gasifier cylinder, the primary gasification fan is connected to the circular kiln hood of the countercurrent rotary primary gasifier through a tangential air duct, the secondary gasification fan is connected to the lower part of the vertical secondary gasifier through an annular tangential air duct, the oxygen meter is located at the horizontal section of the synthesis gas outlet pipeline of the countercurrent rotary primary gasifier, and the synthesis gas component analyzer is located at the horizontal section of the synthesis gas outlet pipeline of the countercurrent rotary primary gasifier; the present invention realizes the graded gasification and segmented control of organic hazardous waste, strengthens the whole process regulation of gasification of various types of organic hazardous waste, improves the material universality of the device and system, and the gasification efficiency is significantly higher than the existing thermochemical treatment technology; the gasification process also realizes ash self-melting, greatly reduces the installed capacity and operating power of the plasma torch, and effectively reduces the investment and operating costs of the industrial application of plasma gasification melting.

[0055] The above is only a preferred embodiment of the present invention and does not limit the present invention in any form. Although the present invention has been disclosed as a preferred embodiment as above, it is not used to limit the present invention. Any technician familiar with this profession can make some changes or modify the technical contents disclosed above into equivalent embodiments without departing from the scope of the technical solution of the present invention. However, any simple modification, equivalent replacement and improvement made to the above embodiments without departing from the content of the technical solution of the present invention, based on the technical essence of the present invention, within the spirit and principles of the present invention, still fall within the protection scope of the technical solution of the present invention.

[0056] In the description of the present invention, it should be noted that the orientation or position relationship indicated by the terms "upper" and "lower" etc. is based on the orientation or position relationship shown in the accompanying drawings, and is only for simplifying the description of the present invention, rather than indicating that the components or devices must have a specific orientation or position, and be constructed and operated as such. Therefore, it should not be narrowly understood as a limitation on the present invention.

[0057] In addition, the terms "first", "second" and "third" are only used to facilitate the description of the present invention and cannot be simply understood as indicating or suggesting relative importance or implicitly indicating the number of technical features indicated. Therefore, the features defined as "first", "second" and "third" may explicitly or implicitly include at least one of such features.

[0058] In the present invention, unless otherwise clearly stipulated or limited, the terms "connection", "setting" and the like should be understood in a broad sense. Unless otherwise clearly limited, a person of ordinary skill in the art can understand the meaning of the above terms in the present invention in combination with specific circumstances.

Claims

1. An integrated plasma multi-stage gasification and melting furnace device for organic hazardous waste, characterized in that: It includes a countercurrent rotary primary gasifier, a vertical secondary gasifier, a molten pool, a spiral feeder for organic hazardous waste, a flux feeder, a burner, a plasma torch, a primary gasifier fan, a secondary gasifier fan, an oxygen meter and a synthesis gas component analyzer; the countercurrent rotary primary gasifier includes a horizontal rotary furnace body, a kiln tail hood, a kiln head hood, a synthesis gas outlet pipe, an emergency chimney, a kiln tail sealing system, a kiln head sealing system and a kiln head sight glass; the angle between the axial center line of the horizontal rotary furnace body and the horizontal line is 2 to 4°; the kiln tail sealing system and the kiln head sealing system are arranged at the connection between the horizontal rotary furnace body and the kiln tail hood and the kiln head hood, which together constitute the countercurrent rotary primary gasifier sealing system, so that the air leakage of the primary gasifier is controlled within 2%; The emergency chimney and the synthesis gas outlet are centrally arranged on the kiln tail hood, and the synthesis gas outlet is connected to the secondary combustion chamber inlet through a synthesis gas outlet pipe; the kiln head sight glass is arranged on the kiln head hood panel and intersects with the axial center line of the horizontal rotating furnace body, so as to facilitate observation of the gasification reaction process of organic hazardous waste in the primary gasifier, and is beneficial to assist in adjusting the primary gasification process conditions and operating parameters; the vertical secondary gasifier includes a vertical cylindrical furnace body and a sight glass; the top of the vertical cylindrical furnace body is connected to the bottom of the kiln head hood of the primary gasifier through a flange; the sight glass is arranged at the lower part of the vertical cylindrical furnace body, so as to facilitate observation of the high-temperature gasification and melting process of solid semi-coke plasma in the secondary gasifier, and is beneficial to assist in adjusting the secondary gasification melting process conditions and operating parameters.

2. The organic hazardous waste integrated plasma multi-stage gasification and melting furnace device according to claim 1 is characterized in that: The molten pool comprises a flat cylindrical body and a slag outlet; the top of the flat cylindrical body is connected to the bottom of the secondary gasifier through a flange.

3. The organic hazardous waste integrated plasma multi-stage gasification and melting furnace device according to claim 1 is characterized in that: The organic hazardous waste spiral feeding device is connected to the kiln tail hood of the countercurrent rotary primary gasifier; the flux feeding device is connected to the kiln head hood of the countercurrent rotary primary gasifier; the burner is arranged in the middle of the kiln head hood panel of the countercurrent rotary primary gasifier; the plasma torch is located at the lower part of the vertical secondary gasifier cylinder; the primary gasification fan is connected to the circular kiln head hood of the countercurrent rotary primary gasifier through the air duct, and the primary gasification wind enters the primary gasifier tangentially to increase the air turbulence in the primary gasifier; the secondary gasification fan is connected to the lower part of the vertical secondary gasifier through the annular air duct; the oxygen meter is located in the horizontal section of the synthesis gas outlet pipeline of the countercurrent rotary primary gasifier; the synthesis gas component analyzer is located in the horizontal section of the synthesis gas outlet pipeline of the countercurrent rotary primary gasifier.

4. The organic hazardous waste integrated plasma multi-stage gasification and melting furnace device according to claim 1 is characterized in that: The counter-current rotary type primary gasifier is provided with a first temperature sensor and a second temperature sensor at the kiln tail hood and the kiln head hood respectively; and a third temperature sensor is provided at the lower part of the vertical secondary gasifier.

5. The organic hazardous waste integrated plasma multi-stage gasification and melting furnace device according to claim 1 is characterized in that: The counter-current rotary type primary gasifier is provided with a first pressure sensor and a second pressure sensor at the kiln tail hood and the kiln head hood respectively; and a third pressure sensor is provided at the lower part of the vertical secondary gasifier.

6. The organic hazardous waste integrated plasma multi-stage gasification and melting furnace device according to claim 3 is characterized by: The primary gasification blower and the secondary gasification blower are both frequency-converting controlled to automatically adjust the primary gasification air volume and the secondary gasification air volume, thereby realizing the oxygen content control of the organic hazardous waste integrated plasma multi-stage gasification melting furnace device.

7. The organic hazardous waste integrated plasma multi-stage gasification and melting furnace device according to claim 3 is characterized by: The burner adopts a split structure, and the burner power and the first temperature sensor form a control loop to automatically adjust the burner auxiliary fuel flow and the burner fan combustion air flow to achieve the device start-up and shutdown furnace temperature control and the first-stage gasification furnace gasification temperature control during normal operation.

8. The organic hazardous waste integrated plasma multi-stage gasification and melting furnace device according to any one of claims 1 to 7, characterized in that: The device comprises an organic hazardous waste integrated plasma multi-stage gasification and melting furnace as described in any one of claims 1 to 7, and 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, and a sewage treatment system, wherein the discharge port of the pretreatment system is connected to the feed port of the spiral feed device of the organic hazardous waste integrated plasma multi-stage gasification and melting furnace device, the synthesis gas outlet pipeline of the organic hazardous waste integrated plasma multi-stage gasification and melting furnace device is connected to the synthesis gas inlet of the secondary combustion chamber, the flue gas outlet of the secondary combustion chamber is connected to the flue gas inlet of the waste heat recovery device, the flue gas outlet of the waste heat recovery device is connected to the flue gas inlet of the flue gas purification device, the flue gas outlet of the flue gas purification device is connected to the flue gas inlet of the induced draft fan, and the flue gas outlet of the induced draft fan is connected to the chimney inlet, so as to achieve standard emission of waste gas; The fly ash generated by the waste heat recovery device and the flue gas purification device is collected and granulated for pre-treatment, and then returned to the vertical secondary gasification furnace for melting and disposal by the flux feeding device. The wastewater generated by the flue gas purification device is pumped to the sewage treatment system for treatment.

9. The organic hazardous waste integrated plasma multi-stage gasification and melting furnace device according to claim 8, characterized in that: The flue gas purification device comprises an SNCR denitration device, a quenching device, a dry deacidification device, an activated carbon injection device, a bag dust removal device, a precooling tower, a two-stage wet deacidification tower, a wet electrostatic precipitator, a GGH flue gas heat exchanger, an SGH flue gas reheater, and an SCR denitration device, wherein the flue gas outlet of the quenching device and the activated carbon outlet of the activated carbon injection device are connected to the flue gas inlet of the dry deacidification device, the flue gas outlet of the dry deacidification device is connected to the flue gas inlet of the bag dust removal device, the flue gas outlet of the bag dust removal device is connected to the flue gas inlet of the precooling tower, and the flue gas outlet of the precooling tower is connected to the flue gas inlet of the first-stage wet deacidification tower. The flue gas outlet of the first wet deacidification tower is connected to the flue gas inlet of the second wet deacidification tower, the flue gas outlet of the second wet deacidification tower is connected to the flue gas inlet of the wet electrostatic precipitator, the flue gas outlet of the wet electrostatic precipitator is connected to the original flue gas inlet of the GGH flue gas heat exchanger, the original flue gas outlet of the GGH flue gas heat exchanger is connected to the flue gas inlet of the SGH flue gas reheater, the flue gas outlet of the SGH flue gas reheater is connected to the flue gas inlet of the SCR denitrification device, the flue gas outlet of the SCR denitrification device is connected to 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 to the flue gas inlet of the induced draft fan, the flue gas is pressurized by the induced draft fan and discharged into the atmosphere through the chimney to achieve standard emission of waste gas.

10. An integrated plasma multi-stage gasification and melting furnace method for organic hazardous waste, characterized in that The following steps are involved: Step 1: Organic hazardous waste is transported through the kiln tail hood by the spiral feeding device into the countercurrent rotary primary gasifier, and the organic hazardous waste and the combustion-supporting air in the furnace are in a state of opposite motion; the spiral feeding device adopts frequency conversion control to adjust the feeding rate; according to the temperature measurement value of the first temperature sensor, the burner power is automatically adjusted to control the gasification temperature of the primary gasifier; the primary gasification fan adopts frequency conversion control to adjust the primary gasification air volume to ensure that the primary gasifier forms an obvious oxygen concentration gradient along the axial direction, thereby realizing the oxygen content control of the organic hazardous waste integrated plasma multi-stage gasification melting furnace device; the countercurrent rotary primary gasifier rotation drive system adopts frequency conversion control to automatically adjust the waste residence time of the primary gasifier, thereby controlling the gasification reaction time of the primary gasifier; a variety of organic hazardous wastes with complex components are comprehensively During gasification, by balancing and adjusting the feed rate, primary gasification air volume, auxiliary fuel volume, gasification temperature ~ 1000℃, gasification reaction time, synthesis gas oxygen content 0.2% ~ 1%, synthesis gas CO concentration 7% ~ 12%, synthesis gas CH4 concentration less than 1%, the organic hazardous waste undergoes drying, rapid pyrolysis, and rapid gasification stages in the primary gasifier, and the high-boiling point, difficult-to-decompose organic matter is completely converted into H2, CO and CH4 synthesis gas, which fundamentally solves the problem of slow processing process of traditional pyrolysis gasification technology. The synthesis gas enters the secondary combustion chamber for gaseous homogeneous combustion, and the reliability and stability of the secondary combustion chamber are significantly enhanced, and the waste heat recovery efficiency of the waste heat recovery device is greatly improved; the solid semi-coke produced by the primary gasifier falls into the vertical secondary gasifier as the primary gasifier rotates, so that the solid semi-coke is further processed; Step 2: Solid semi-coke forms a material bed layer of a certain height in the vertical secondary gasifier, and flux and coke are added to the vertical secondary gasifier through the flux feeding device. The difference in specific gravity of coke causes it to gather between the material bed layer and the molten slurry to form a coke bed layer. The coke bed layer provides support for the material bed layer and guides the plasma jet into the material bed layer. The coke bed layer provides a pore channel for the downward flow of slag and metal; the high temperature and high reaction activity of the plasma make the fixed carbon in the solid semi-coke quickly gasify into CO, so that the ash in the solid semi-coke is self-melted during the high-temperature rapid gasification process of the plasma; the high-temperature synthesis gas generated by the vertical secondary gasifier is used as a partial heat source of the countercurrent rotary primary gasifier, which can significantly accelerate the primary gasification reaction process; according to the temperature measurement value of the second temperature sensor, the plasma torch power and the secondary gasification air volume are automatically adjusted , thereby controlling the secondary gasification temperature and realizing rapid gasification of solid semi-coke, solving the problems of slow reaction process and incomplete reaction of solid semi-coke in traditional thermochemical treatment technology; at the same time, by adjusting the type and amount of flux, the ash melting point temperature of ash content can be effectively reduced to improve the fluidity of slurry, thereby reducing the energy consumption of the system; when the slurry in the molten pool reaches a certain material level, the slurry is discharged out of the furnace through the slag outlet of the molten pool at the bottom of the secondary gasifier, and after water quenching and cooling, a glassy substance is formed, which is used as a general solid waste for resource utilization, avoiding the generation of secondary hazardous waste; through steps one and two, hierarchical gasification and segmented control of organic hazardous waste are realized, the process adjustment and control of the whole gasification process are strengthened, the material adaptability and gasification efficiency of the device and system are significantly improved, the prerequisite for dioxin synthesis is eliminated, and the dioxin pollution problem is solved from the source; Step 3: Synthesis gas is efficiently homogeneously burned in the secondary combustion chamber, releasing a large amount of heat without the need to add auxiliary fuel, thereby maintaining the operating temperature of the secondary combustion chamber ≥ 1100°C; the high-temperature flue gas from the secondary combustion chamber enters the waste heat recovery device for waste heat power generation or steam utilization, which can improve the economic efficiency of system operation; before the country releases special technical specifications and pollution control standards for plasma technology to treat hazardous waste, the 500°C flue gas after waste heat recovery needs to enter the quenching device to rapidly cool down to less than 200°C within 1 second to avoid the temperature range of dioxin resynthesis; Step 4: The flue gas rapidly cooled by the quenching device enters the dry deacidification device to remove part of the acid gases such as SO2, HCl and HF. The flue gas after dry deacidification is adsorbed by activated carbon to remove heavy metals and dioxins, and then filtered by a bag dust removal device to remove most of the particulate matter; the flue gas after dust removal is further removed by a precooling tower and a two-stage wet deacidification tower to remove acid gases such as SO2, HCl and HF. The flue gas after wet deacidification is further removed by a wet electrostatic precipitator to remove particulate matter, acid mist and salt mist; Step 5: The flue gas at the outlet of the wet electrostatic precipitator is heated to 140°C by the GGH flue gas heat exchanger; the flue gas outlet of the wet electrostatic precipitator is connected to the original flue gas inlet of the GGH flue gas heat exchanger, and the flue gas outlet of the SCR denitrification device is connected to the clean flue gas inlet of the GGH flue gas heat exchanger. After the high-temperature flue gas and the low-temperature flue gas are heat exchanged, the flue gas temperature at the original flue gas outlet of the GGH flue gas heat exchanger rises to 140°C, and the flue gas temperature at the clean flue gas outlet of the GGH flue gas heat exchanger drops to 130°C, so as to achieve the purpose of recovering the waste heat of the SCR denitrification flue gas and reducing the energy consumption of the system; Step 6: The flue gas heated by GGH is further heated to about 200℃ by SGH flue gas reheater. SGH flue gas reheater uses 300℃ superheated steam generated by waste heat recovery device to heat the flue gas to 200℃ to meet the working temperature requirements of SCR denitrification device; the flue gas at the outlet of SGH flue gas reheater enters SCR catalytic denitrification device for further deep removal of NO X ; Step 7: The clean flue gas outlet of the GGH flue gas heat exchanger is connected to the induced draft fan inlet, and the clean flue gas is pressurized by the induced draft fan and discharged into the atmosphere through the chimney.

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