CN112856455B - High-nitrogen high-sulfur gelatinous asphaltene hazardous waste gasification incineration system and method - Google Patents
High-nitrogen high-sulfur gelatinous asphaltene hazardous waste gasification incineration system and method Download PDFInfo
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- 238000002309 gasification Methods 0.000 title claims abstract description 178
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 56
- 239000011593 sulfur Substances 0.000 title claims abstract description 53
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 50
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 43
- 238000000034 method Methods 0.000 title claims abstract description 42
- 239000002920 hazardous waste Substances 0.000 title claims abstract description 33
- 238000002485 combustion reaction Methods 0.000 claims abstract description 135
- 239000000463 material Substances 0.000 claims abstract description 129
- 239000007789 gas Substances 0.000 claims abstract description 84
- 239000002699 waste material Substances 0.000 claims abstract description 57
- 239000007787 solid Substances 0.000 claims abstract description 28
- 239000000126 substance Substances 0.000 claims abstract description 24
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 22
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000000889 atomisation Methods 0.000 claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 13
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 10
- 238000005243 fluidization Methods 0.000 claims abstract description 10
- 239000003345 natural gas Substances 0.000 claims abstract description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 7
- 238000009826 distribution Methods 0.000 claims description 46
- 239000003546 flue gas Substances 0.000 claims description 43
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 42
- 238000011084 recovery Methods 0.000 claims description 25
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 24
- 239000011261 inert gas Substances 0.000 claims description 19
- 229910052760 oxygen Inorganic materials 0.000 claims description 18
- 239000007921 spray Substances 0.000 claims description 17
- 239000011343 solid material Substances 0.000 claims description 14
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 13
- 239000001301 oxygen Substances 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 238000007599 discharging Methods 0.000 claims description 10
- 238000003860 storage Methods 0.000 claims description 9
- 230000007613 environmental effect Effects 0.000 claims description 8
- 239000002283 diesel fuel Substances 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 7
- 238000010793 Steam injection (oil industry) Methods 0.000 claims description 5
- 239000002893 slag Substances 0.000 claims description 5
- 239000000446 fuel Substances 0.000 claims description 4
- 229910052739 hydrogen Inorganic materials 0.000 claims description 4
- 206010021143 Hypoxia Diseases 0.000 claims description 3
- 238000012840 feeding operation Methods 0.000 claims description 3
- 230000007954 hypoxia Effects 0.000 claims description 3
- 239000002956 ash Substances 0.000 abstract description 96
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 29
- 239000006229 carbon black Substances 0.000 abstract description 12
- 239000000084 colloidal system Substances 0.000 abstract description 2
- 238000004056 waste incineration Methods 0.000 abstract description 2
- 235000002918 Fraxinus excelsior Nutrition 0.000 abstract 1
- 238000000197 pyrolysis Methods 0.000 abstract 1
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 10
- 239000000779 smoke Substances 0.000 description 9
- 238000004880 explosion Methods 0.000 description 8
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 7
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 6
- 235000011130 ammonium sulphate Nutrition 0.000 description 6
- 239000003054 catalyst Substances 0.000 description 6
- 238000004064 recycling Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000006004 Quartz sand Substances 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 125000001477 organic nitrogen group Chemical group 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 238000005411 Van der Waals force Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000010426 asphalt Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000010882 bottom ash Substances 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000004200 deflagration Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- -1 flue gas nitrogen oxides Chemical class 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 231100001261 hazardous Toxicity 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 238000010943 off-gassing Methods 0.000 description 1
- 235000011837 pasties Nutrition 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- 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
- F23G5/44—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
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/50—Control or safety arrangements
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Gasification And Melting Of Waste (AREA)
Abstract
The invention provides a high-nitrogen high-sulfur gelatinous asphaltene dangerous waste gasification incineration system and a method. The system comprises a feeding system, a gasification system, an incineration system and a clinker collecting system, wherein the invention adopts bed materials to participate in gasification, and the hazardous waste is sprayed into a gasification furnace in an atomization mode after being heated into a liquid form, the gasification system forms a gasification mode of a circulating fluidized bed through a connection mode among the gasification furnace, a cyclone separator and a material returning device, so that organic substances in the hazardous waste are partially combusted to provide energy for gasification and pyrolysis, the hazardous waste and the bed materials are mixed together through fluidization wind to gasify and crack to generate organic combustible gas in a high-temperature state, and solid carbon, tar and other substances generated by incomplete gasification in the gasification process. Solves the technical problems of extremely high nitrogen and high sulfur colloid asphaltene in the prior art that nitrogen oxides generated by dangerous waste incineration are easy to deflagrate during combustion, natural gas consumption in a secondary combustion chamber is too high, and organic carbon black which is difficult to burn out and form ashes is burnt out.
Description
Technical Field
The invention relates to an environmental protection treatment technology for chemical hazardous waste incineration, in particular to a gasification incineration system and method for high-nitrogen high-sulfur gelatinous asphaltene hazardous waste, belonging to the field of energy conservation and environmental protection.
Background
At present, one or more kinds of high-nitrogen high-sulfur normal-temperature solid and heated liquid high-viscosity dangerous wastes generated in the production process of chemical industry, rubber industry, petroleum refining and petrochemical industry, medical manufacturing industry, coating and printing ink industry, plastic product manufacturing industry and other industries have the characteristics of high heat value, high nitrogen content, high sulfur content, normal-temperature solid crushing and explosion easiness, poor liquid high-viscosity fluidity and the like, and have the dangerous characteristics of inflammability, explosion easiness, toxicity, harm and the like, carbon black is easy to separate out during combustion, and the dangerous wastes belong to dangerous wastes.
The method for treating the waste of the type in China is generally an incineration mode, some adopts a fixed hearth furnace for incineration, some adopts a chamber combustion furnace, most adopts a rotary kiln and a secondary combustion chamber, and other adopts a fluidized bed or circulating fluidized bed incineration mode, but basically cannot reliably operate, and all the problems of difficult feeding into the furnace, large amount of precipitated carbon black, deflagration, extremely high generation amount of flue gas nitrogen oxides, serious equipment corrosion and the like exist. Methods and means for efficient incineration disposal have not been found to date.
The prior incineration method mainly solves the problems of the high-nitrogen high-sulfur normal-temperature solid, heated liquid and high-viscosity hazardous waste in the incineration process, and is characterized in that:
(1) Most of the wastes are solid at normal temperature, become soft and sticky when heated to about 30-40 ℃, exist in pasty, asphalt-like and other sticky states at above 60 ℃, and are broken at normal temperature or after freezing due to the high sulfur content and high heat value of the wastes and explosion danger during breaking.
(2) The waste has poor fluidity and high viscosity when the heating temperature is low, but is easy to crack to generate combustible gas, is very difficult to enter a furnace and atomize, and is easy to cause the problems of blockage of a feed pipe (mouth) and an atomizing spray gun, poor atomizing quality and the like.
(3) The waste has higher nitrogen content, higher heat value, very high combustion temperature during incineration, particularly high fuel-type and thermal-type nitrogen oxide generation amount, and increased investment cost and operation cost of a later-stage denitration device.
(4) The waste has high sulfur content, and the waste needs to react under the condition of oxygen enrichment and high temperature during incineration to convert the sulfur in the waste into sulfur dioxide; and the sulfur dioxide reacts with ammonia generated by the sprayed denitration reducing agent to form ammonium sulfate in the subsequent denitration treatment process, so that the method has great influence: A. sulfur dioxide corrodes the SCR denitration catalyst, so that the SCR denitration catalyst loses activity; B. the ammonium sulfate is attached to the surface of the denitration catalyst to block the SCR denitration catalyst from contacting with the flue gas, so that the denitration catalyst is deactivated; C. the ammonium sulfate not only blocks the flue gas channel of the denitration catalyst, but also blocks the flue gas channel of other equipment, thereby affecting the stable operation of the system, and as the ammonium sulfate is a flammable and explosive chemical, a certain amount of the ammonium sulfate is accumulated in the system and can cause explosion at a certain temperature; D. the ammonium sulfate is discharged and collected to be new dangerous waste, so that secondary pollution is caused, and secondary environmental protection treatment is also needed.
(5) If sulfur recovery or sulfuric acid recovery is to be carried out, the recovered sulfur and sulfuric acid contains nitric acid and ammonium sulfate salt generated in the denitration process, so that the purity of sulfuric acid or sulfur byproducts is seriously influenced, even the condition that the sulfuric acid or sulfur byproducts cannot be sold or reused is possibly caused, and the sulfuric acid or sulfur byproducts need to be reprocessed, so that secondary burden is caused to enterprises.
(6) The waste is generally in a macromolecular structure, has higher C atom content (generally more than C8), can be quickly expanded due to heating after entering the incinerator, becomes sticky and is burnt with the incinerator, so that the air distribution of the incineration is disordered, a fire hole appears, oxygen enrichment exists in some places and oxygen depletion exists in some places, a large amount of carbon black, tar particles and unburned combustible gases such as CO, CH 4 and the like can be separated out to enter subsequent equipment, and the flue gas is difficult to reach the environment-friendly emission standard.
Disclosure of Invention
Aiming at the problems that the high-nitrogen high-sulfur gelatinous asphaltene dangerous waste is difficult to treat and the incineration treatment is poor, the invention provides a high-nitrogen high-sulfur gelatinous asphaltene dangerous waste gasification incineration system and a high-nitrogen high-sulfur gelatinous asphaltene dangerous waste gasification incineration method, so as to realize the effective and reliable method for carrying out environmental protection, harmless and recycling treatment on the high-nitrogen high-sulfur gelatinous asphaltene dangerous waste.
In order to achieve the above purpose, the invention adopts the following technical scheme:
The technical purpose of the first aspect of the invention is to provide a high-nitrogen high-sulfur gelatinous asphaltene dangerous waste gasification incineration system, which comprises a feeding system, a gasification system, an incineration system and an ash collection system;
The feeding system comprises a bed material feeding device and a hazardous waste feeding device, wherein the bed material feeding device comprises a vibrating screen, a bed material storage bin and a bed material feeding pipe, and the hazardous waste feeding device comprises a booster pump, an atomizing spray gun and a conveying pipeline connected with the booster pump and the atomizing spray gun, and the conveying pipeline is used for laying a steam tracing pipeline along the path;
The gasification system comprises a gasification furnace, a cyclone separator and a material returning device, wherein an atomization spray gun and a bed material feeding pipe of the material feeding system are respectively connected to respective inlets of the gasification furnace, a wind distribution plate is arranged at the inner bottom of the gasification furnace, a wind distribution chamber is separated from a gasification reaction chamber through the wind distribution plate, the inlet of the atomization spray gun is arranged on the gasification chamber, the inlet of the bed material feeding pipe is arranged above the wind distribution plate, a wind cap is arranged on the wind distribution plate to communicate the wind distribution chamber with the gasification chamber, one end of the wind distribution chamber is connected with one end of a furnace starting burner of the gasification furnace, the other end of the furnace starting burner is connected with a natural gas or light diesel fuel interface and a fluidized wind distribution interface, an outlet at the upper part of the gasification chamber of the gasification furnace is connected with the cyclone separator through a flue, solid materials separated by the cyclone separator enter a material returning device connected with a material leg, an outlet of the material returning device is connected to the gasification chamber of the gasification furnace, a wind cap and the wind distribution plate are also arranged in the material returning device, high-pressure inert gas is adopted to perform material loosening and feeding on the solid materials entering the material returning device through the wind cap, and the material returning device in the gasification chamber;
The incineration system comprises a secondary combustion chamber connected with a combustible gas outlet flue generated by gasification of gas-solid separation of the cyclone separator, the secondary combustion chamber is also connected with a secondary combustion chamber blower through a gas distribution pipeline, a combustor is arranged at an inlet of the secondary combustion chamber, a flue gas outlet is arranged at the lower part of the secondary combustion chamber, and a secondary combustion chamber ash bucket and a secondary combustion chamber ash bin are sequentially arranged at the bottom of the secondary combustion chamber;
The ash collection system comprises a gasifier ash and slag recovery device, a returning charge ash recovery device and a secondary combustion chamber ash recovery device, wherein the gasifier ash and slag recovery device comprises a gasifier ash discharge pipe connected with an ash outlet at the bottom of the gasifier, the gasifier ash discharge pipe is connected with a gasifier ash replacement bin through a gasifier ash discharge valve, the gasifier ash replacement bin is provided with an inert gas inlet for replacing combustible gas in gasifier ash and a replaced combustible gas outlet, the combustible gas outlet is connected to the secondary combustion chamber through a pipeline, the replaced combustible gas is incinerated in the secondary combustion chamber, and solids replaced in the gasifier ash replacement bin are connected to a vibrating screen through a conveying device; the ash recovery device of the material returning device comprises an ash discharging pipe of the material returning device, which is connected with an ash discharging valve of the material returning device, and is connected with an ash replacing bin of the material returning device, wherein the ash replacing bin of the material returning device is provided with an inlet of inert gas for replacing combustible gas in ash of the ash replacing bin of the material returning device and an outlet of replaced combustible gas, the outlet of the combustible gas is connected to a secondary combustion chamber through a pipeline, the replaced combustible gas in the secondary combustion chamber is incinerated, and solids replaced in the ash replacing bin of the material returning device are connected to a vibrating screen through a conveying device; the ash recovery device of the secondary combustion chamber comprises an ash bucket and an ash bin which are arranged at the bottom of the secondary combustion chamber, and an outlet of the ash bin is connected with a vibrating screen through a conveying device.
Further, one or more steam injection ports are arranged in a dense-phase area at the lower part of the gasification furnace, a gasification gas temperature measuring point is arranged at an outlet at the upper part of a gasification chamber of the gasification furnace, water vapor can be sprayed into the gasification furnace according to the gasification gas temperature measured by the gasification gas temperature measuring point and the air distribution quantity of the gasification furnace so as to control the temperature of the gasification furnace, and meanwhile, the injection of the water vapor is beneficial to gasification reaction, so that H, O is provided for the gasification reaction to generate CH 4、CO、H2 S;
Further, a smoke temperature measuring point is arranged at a smoke outlet at the lower part of the secondary combustion chamber, air can be supplemented into the secondary combustion chamber according to the smoke temperature measured by the smoke temperature measuring point at the smoke outlet of the secondary combustion chamber, when the smoke temperature is reduced during air supplementing, a secondary combustion chamber burner with a pilot burner is started to assist in burning natural gas or light diesel oil, so that the smoke temperature measured by the smoke temperature measuring point at the smoke outlet of the secondary combustion chamber is not lower than 1100 ℃, and the complete burning of organic components in gasification gas is ensured;
Further, the bed material feeding device also comprises necessary material conveying devices, in particular a bucket elevator connected between the vibrating screen and the bed material storage bin and a screw conveyor connected between the bed material storage bin and the bed material feeding pipe.
Further, a fluidization hood is arranged on an air distribution plate in the gasification furnace, and air distribution in the air distribution chamber is led into the gasification reaction chamber to carry out gasification reaction.
Further, the air quantity and the air pressure of the Roots blower are controlled according to the temperature in the gasification furnace.
Further, safety devices such as explosion doors and the like are further arranged in the secondary combustion chamber. In addition, in order to ensure safety, the burner is a pilot burner.
The burner of the secondary combustion chamber is a natural gas or light diesel burner.
The technical purpose of the second aspect of the invention is to provide a method for gasifying and incinerating high-nitrogen high-sulfur gelatinous asphaltene dangerous waste by using the system, which comprises the following steps:
The bed material is put into a gasification furnace through a bed material feeding device, high-nitrogen high-sulfur gelatinous asphaltene dangerous waste is changed into a liquid form with good fluidity after being subjected to steam tracing treatment in a conveying pipeline, the liquid dangerous waste is conveyed to an inlet of an atomization spray gun through a booster pump, the liquid dangerous waste is sprayed into the gasification furnace after being atomized, high-pressure air is introduced into the gasification furnace through a Roots blower of the gasification furnace, the amount of the introduced high-pressure air is 0.2-0.35 times of the air amount required by complete combustion of the dangerous waste, a hypoxia environment is formed, the high-pressure air enables the dangerous waste and the bed material to be fluidized and mixed in the gasification furnace, a part of the dangerous waste is combusted in the environment of high-pressure fluidization wind, oxygen in the high-pressure fluidization wind is completely consumed, a large amount of heat is discharged, energy is provided for gasification of another part of dangerous waste, and C, H, O, N and S in the dangerous waste are converted into N 2、H2S、CO、CO2, a small amount of SO 2、H2 and other mixed organic combustible gases in the gasification process;
The organic combustible gas, the thermal-state bed material, solid carbon, tar and other substances generated by incomplete gasification enter a cyclone separator connected with the gasification furnace through an outlet flue at the upper part of the gasification furnace, gas-solid separation is carried out on the combustible gas generated by gasification, the separated solid materials enter a material returning device connected with a material leg through a material leg at the lower part of the cyclone separator, the solid materials of the material leg are loosened through loose air, and the solid materials entering the material returning device are returned to the gasification furnace through feeding air to carry out gasification reaction again, so that the gasification furnace, the cyclone separator and the material returning device form a gasification mode of a circulating fluidized bed; the loosening air and the feeding air are high-pressure inert gases;
The organic combustible gas separated by the cyclone separator is conveyed to a secondary combustion chamber through a flue, combustion air is fed into the secondary combustion chamber through a secondary combustion chamber blower, so that the organic combustible gas is combusted in the secondary combustion chamber, and high-temperature flue gas after combustion is discharged from a flue gas outlet of the secondary combustion chamber;
When ash is needed to be removed, the ash discharging valve of the gasifier is closed, inert gas is introduced into the ash replacing bin of the gasifier, organic combustible gas carried in ash in the ash replacing bin of the gasifier is replaced by the inert gas, the organic combustible gas is replaced and discharged and conveyed to a secondary combustion chamber, the secondary combustion chamber is burnt, and solids are conveyed to a vibrating screen through a conveying device; the ash and the bed material in the material returning device are treated in the same way as the ash and the bed material in the gasification furnace; ash in the secondary combustion chamber falls into the ash bin of the secondary combustion chamber from the ash hopper of the secondary combustion chamber positioned at the bottom of the secondary combustion chamber, and is then conveyed to the vibrating screen through the conveying device.
Further, the bed material adopts quartz sand with the diameter of 3mm plus or minus 1 mm.
Further, the atomization is atomization by adopting low-pressure steam or compressed air as an atomization medium or direct pressure atomization without the atomization medium.
Further, when the furnace starting burner of the gasification furnace is used for baking and starting the furnace, the bed material on the air distribution plate in the gasification furnace is heated by burning natural gas or light diesel oil, and when the bed material is heated to over 650 ℃, the feeding operation is started. The gasification furnace burner burns auxiliary fuel to perform new furnace baking and energy is provided when starting the furnace, the bed material is heated to about 650-850 ℃ and then the feeding operation is started.
Further, the gasification temperature of the gasification furnace is controlled to be about 850 ℃, and the temperature control is mainly realized by controlling the air quantity and the air pressure of the Roots blower and the steam sprayed into the gasification furnace, so that the temperature in the gasification furnace can be increased by increasing the air quantity and the air pressure, and the temperature in the gasification furnace can be reduced by spraying the steam.
Further, the flue gas outlet of the secondary combustion chamber is provided with an oxygen meter, the organic combustible gas generated by the gasifier burns in the secondary combustion chamber, the flow of the blown combustion air is regulated by controlling the opening of the air regulating door of the air distribution blower of the secondary combustion chamber according to the measured value of the oxygen meter of the flue gas outlet of the secondary combustion chamber, the dry oxygen content in the combusted flue gas is ensured to be 6-10%, so that the organic combustible gas generated by the gasifier is ensured to fully burn in the secondary combustion chamber, the burner acts as a pilot lamp, the combustion is ensured to be safe and reliable, and the secondary combustion chamber burner is started when the flue gas temperature at the outlet of the secondary combustion chamber is lower than 1100 ℃, the condition requirement that the flue gas temperature at the outlet of the secondary combustion chamber is more than or equal to 1100 ℃ is met, and the requirement of the sufficient environmental protection standard is ensured to be met.
Further, the organic combustible gas discharged from the gasifier ash replacement bin and the returning charge ash replacement bin is also conveyed to the secondary combustion chamber through a pipeline for incineration.
Further, the gas introduced into the return device, the gasifier ash replacement bin and the return device ash replacement bin is inert gas, preferably N 2.
Further, the method also comprises the step of sending the flue gas generated after the combustion of the secondary combustion chamber into a lower-level tail gas environment-friendly treatment system and carrying out tail gas treatment by a sulfur or sulfuric acid recovery system.
Compared with the prior art, the high-nitrogen high-sulfur gelatinous asphaltene hazardous waste gasification incineration system and method have the following advantages:
(1) The system adopts a method of firstly gasifying high-nitrogen high-sulfur gelatinous asphaltene dangerous waste and then burning combustible gas generated by gasification to treat the high-nitrogen high-sulfur gelatinous asphaltene dangerous waste, converts organic nitrogen in chemical dangerous waste into N 2, and reduces the formation of fuel-type nitrogen oxides during combustion. If the high-nitrogen high-sulfur gelatinous asphaltene is directly combusted, the formation amount of organic nitrogen converted into nitrogen oxides in the high-nitrogen high-sulfur gelatinous asphaltene dangerous waste is extremely large, the subsequent environmental protection treatment is extremely difficult, and the emission is difficult to reach the standard. Meanwhile, because the gasification adopts the anaerobic incineration, the incineration part of organic matters provides energy for the gasification SO as to generate organic combustible gas as a main part, and the gasification process of high-sulfur organic matters is mainly converted into H 2 S SO as to generate a small amount of SO 2, thus the corrosion to a gasification system is reduced.
(2) The system adopts the method that the high-nitrogen high-sulfur gelatinous asphaltene hazardous waste is gasified first and then the combustible gas generated by gasification is combusted, thereby reducing a large amount of auxiliary fuel required by secondary combustion and reducing the operation cost of treating the high-nitrogen high-sulfur gelatinous asphaltene hazardous waste.
(3) The system adopts the circulating fluidized bed gasifier to gasify the high-nitrogen high-sulfur colloidal asphaltene dangerous waste, so that carbon black precipitation of the high-nitrogen high-sulfur colloidal asphaltene dangerous waste can be effectively eliminated. If high-nitrogen high-sulfur gelatinous asphaltene dangerous waste with high heat value is directly combusted, a large amount of carbon black is precipitated, so that the ringelman blackness of the discharged flue gas is increased and is not up to the standard, energy waste is caused by unburnt carbon black, meanwhile, the precipitated carbon black is fine particles, the effects of static electricity, van der Waals force, force among molecules and the like exist among the fine particles, a large amount of carbon black is easy to deposit in a flue gas runner of a system, the danger of explosion of the system and the flue gas runner exists, and potential safety hazards exist. Therefore, the circulating fluidized bed and the gasification mode are adopted, so that the generation of nitrogen oxides is effectively reduced, the generation of sulfur dioxide is also lightened, the precipitation of carbon black is eliminated, and the safe, reliable, environment-friendly and energy-saving operation of the system is ensured.
(4) The system and the method adopt the steps that high-nitrogen high-sulfur gelatinous asphaltene hazardous waste is heated by steam to be liquid and sprayed into the gasification furnace for gasification reaction in an atomization mode, atomized chemical hazardous waste particles are small in size and are mixed with hot bed materials in a scattered fluidization mode, the gasification reaction rate is high, the treatment of chemical hazardous waste organic matters is complete and thorough, and the burning rate is high.
(5) The system and the method adopt the circulating fluidized bed and the bed material to participate in gasification, so that chemical hazardous waste and hot bed material sprayed into the gasification furnace are fully mixed, and the hot bed material and the chemical hazardous waste are in a circulating fluidization reaction process of suspension, cross collision and the like in the whole system, thereby increasing the gasification efficiency of the chemical hazardous waste. Simultaneously, substances such as solid carbon, tar and precipitated carbon black generated by incomplete gasification in the gasification process of macromolecular substances in hazardous waste of the system and the method are fully mixed with bed materials, combustible gas generated by gasification is subjected to gas-solid separation through a gas-solid separator, and the separated substances such as solid carbon, tar and precipitated carbon black are returned into the circulating fluidized bed gasification furnace through a material returning device to be gasified again, so that the organic substances in the chemical hazardous waste are recycled, the organic substances in the chemical hazardous waste are gasified more thoroughly, and the organic substances in the chemical hazardous waste are ensured to be gasified and incinerated thoroughly.
(6) The gasification process in the system and the method ensures that nitrogen is converted into nitrogen instead of nitrogen oxides under the conditions of low temperature and oxygen shortage, ensures that the content of the nitrogen oxides in the finally discharged flue gas reaches the standard, saves a denitration device, reduces the occupied area, reduces the equipment investment cost and the operation cost, and simplifies the system process.
(7) The present system and method can utilize recycled bed material to provide gasification preheating energy for newly-charged waste, thereby reducing the amount of waste to be incinerated, i.e., reducing the amount of air delivered, namely: the nitrogen oxide generation amount can be further reduced, and the running cost can be reduced.
(8) The tail gas finally discharged in the system and the method has low nitrogen oxide content and higher sulfur dioxide content, so that the tail gas can be completely sent to a subsequent system for sulfur recovery or sulfuric acid recovery treatment, and the problem that the purity of sulfur or sulfuric acid is influenced as described in the background art part does not exist.
(9) The ash slag in the system and the method is recycled, no waste water is discharged, and the generated high-temperature flue gas is sent to a subsequent system for sulfur recovery or sulfuric acid recovery treatment, so that no waste is discharged, and no secondary pollution is caused.
(10) The system and the method have the advantages that the public engineering consumes only a small amount of atomizing medium of waste and electricity consumed by the fan, the operation cost is extremely low, the discharged tail gas can be subjected to waste heat recovery and sulfur recovery or sulfuric acid recovery through a subsequent system, the low investment cost and the low operation cost are realized, the high-nitrogen high-sulfur gelatinous asphalt chemical hazardous waste is treated, and meanwhile, steam, sulfur or sulfuric acid are by-produced, so that the hazardous waste is treated for enterprises, and the economic benefit is created for the enterprises.
Drawings
FIG. 1 is a high nitrogen high sulfur gelatinous asphaltene hazardous off-gassing incineration system of example 1;
FIG. 2 is a schematic view of the gasification chamber and the air distribution chamber at the lower end of the gasification furnace in FIG. 1;
Wherein, 1, a bucket elevator; 2. a booster pump; 3. a bed material storage bin; 4. a screw conveyor; 5. a bed material feeding pipe; 6. an atomizing spray gun; 7. starting a gasifier burner; 8. roots blower; 9. a gasification furnace; 10. a cyclone separator; 11. a dipleg; 12. a material returning device; 13. a combustible gas outlet flue generated by gasification; 14. a secondary combustion chamber burner comprising a pilot lamp; 15. a secondary combustion chamber blower; 16. an explosion door; 17. a secondary combustion chamber; 18. a flue gas outlet; 19. a second combustion chamber ash bucket; 20. a secondary combustion chamber ash bin; 21. an ash discharge pipe of the material returning device; 22. an ash discharge valve of the material returning device; 23. a material returning device ash replacing bin; 24. an inlet for inert gas for replacing combustible gas in the ash of the material returning device ash replacement bin; 25. a combustible gas outlet which is replaced by a return ash replacing bin; 26. ash discharge pipe of gasification furnace; 27. an ash discharge valve of the gasifier; 28. a gasifier ash replacing bin; 29. an inert gas inlet for replacing combustible gas in the gasifier ash; 30. a combustible gas outlet which is replaced by the ash residue replacement bin of the gasifier; 31. the device comprises a vibrating screen 32, air distribution plates 33, air distribution chambers 34, a hood 35, a gasification chamber 36, a fluidized air distribution interface 37, a fluidized air distribution channel 38, a fluidized air quantity control air damper 39, fuel interfaces such as natural gas or light diesel oil and the like, a material returning device outlet 40, a steam injection port 41, a steam injection port 42, a gasification gas temperature measuring point 43 and a flue gas temperature measuring point.
Detailed Description
The invention is further illustrated by the following examples:
Example 1
The embodiment discloses a high-nitrogen high-sulfur gelatinous asphaltene dangerous waste gasification incineration system, which is shown in fig. 1 and 2 and comprises a feeding system, a gasification system, an incineration system and an ash collection system;
The feeding system comprises a bed material feeding device and a hazardous waste feeding device, wherein the bed material feeding device comprises a vibrating screen 31, a bucket elevator 1, a bed material storage bin 3, a screw conveyor 4 and a bed material feeding pipe 5 which are sequentially connected, and the hazardous waste feeding device comprises a booster pump 2, an atomizing spray gun 6 and a conveying pipeline connected with the booster pump and the atomizing spray gun, and the conveying pipeline is provided with a steam tracing pipeline along the way;
The gasification system comprises a gasification furnace 9, a cyclone separator 10 and a material returning device 12, an atomization spray gun 6 and a bed material feeding pipe 5 of the material feeding system are respectively connected with respective inlets of the gasification furnace, an air distribution plate 32 is arranged at the inner bottom of the gasification furnace 9, an air distribution chamber 33 is separated from a gasification chamber 35 through the air distribution plate 32, the inlet of the atomization spray gun is arranged on the gasification chamber 35, the inlet of the bed material feeding pipe is arranged above the air distribution plate 32, an air cap 34 is arranged on the air distribution plate 32 to communicate the air distribution chamber 33 with the gasification chamber 35, one end of the air distribution chamber 33 is connected with one end of a furnace starting burner 7 of the gasification furnace, the other end of the furnace starting burner 7 is connected with a natural gas or light diesel fuel interface 39 and a fluidized air distribution interface 36, a fluidized air volume control air regulator 38 is also arranged between the fluidized air distribution interface 36 and the fluidized air distribution channel 37, the upper outlet of the gasification chamber 35 of the gasification furnace is connected with the cyclone separator 10 through a flue, the solid materials separated by the cyclone separator 10 enter a returning device 12 connected with the material leg 11 through a material leg 11 at the lower part of the returning device, a returning device outlet 40 is connected to a gasification chamber 35 of the gasification furnace, a blast cap and a wind distribution plate are also arranged in the returning device 12, high-pressure inert gas is adopted to loosen and feed the solid materials entering the returning device 12 through the blast cap, the loosened materials are aimed at the material leg materials of the cyclone separator 10, the materials in the returning device 12 are fed into the gasification chamber 35 of the gasification furnace, one or more steam injection ports 41 are arranged in a dense phase area at the lower part of the gasification furnace, a gasification gas temperature measuring point 42 is arranged at the upper outlet of the gasification chamber of the gasification furnace, water vapor is injected into the gasification furnace according to the gasification gas temperature measured by the gasification gas temperature measuring point 42 at the outlet of the gasification furnace and the distribution volume of the gasification furnace, meanwhile, the injection of the water vapor is favorable for gasification reaction, h, O is provided for gasification to generate CH 4、CO、H2 S;
The incineration system comprises a secondary combustion chamber 17 connected with a combustible gas outlet flue 13 generated by gasification of gas-solid separation of a cyclone separator 10, the secondary combustion chamber 17 is also connected with a secondary combustion chamber blower 15 through a distribution pipeline, a secondary combustion chamber combustor 14 containing a pilot burner is arranged at an inlet of the secondary combustion chamber, safety devices such as an explosion door 16 and the like are also arranged, a flue gas outlet 18 is arranged at the middle lower part of the secondary combustion chamber 17, a secondary combustion chamber ash bucket 19 and a secondary combustion chamber ash bin 20 are sequentially arranged at the bottom, a flue gas temperature measuring point 43 is arranged at the flue gas outlet 14 at the lower part of the secondary combustion chamber, air is supplemented into the secondary combustion chamber according to the flue gas temperature measured by the flue gas temperature measuring point 43, when the flue gas temperature is reduced, the secondary combustion chamber combustor 14 containing the pilot burner is started, the flue gas temperature measuring point 43 is used for assisting in combusting natural gas or light diesel oil, and the flue gas temperature measured by the flue gas temperature measuring point 43 is not lower than 1100 ℃, and organic components in gasification gas are thoroughly incinerated;
The ash collecting system comprises a gasifier ash recycling device, a returning charge ash recycling device and a secondary combustion chamber ash recycling device, wherein the gasifier ash recycling device comprises a gasifier ash discharging pipe 26 connected with an ash outlet at the bottom of the gasifier, the gasifier ash discharging pipe is connected with a gasifier ash replacing bin 28 through a gasifier ash discharging valve 27, the gasifier ash replacing bin 28 is provided with an inlet 29 for inert gas for replacing combustible gas in gasifier ash and an outlet 30 for combustible gas replaced by the gasifier ash replacing bin, the secondary combustion chamber 17 is connected with the secondary combustion chamber 17 through a pipeline, the replaced combustible gas is burnt in the secondary combustion chamber 17, and solids replaced by the gasifier ash replacing bin 28 are connected with a vibrating screen 31 through a conveying device; the said returning charge ash recovery device includes the returning charge ash discharge tube 21 connected with ash outlet of bottom ash of returning charge, it connects returning charge ash and replaces the storehouse 23 through returning charge ash discharge valve 22, returning charge ash replaces storehouse 23 to have inert gas inlet 24 and returning charge ash replace storehouse replace combustible gas outlet 24 that the storehouse replace, the latter connects to the secondary combustion chamber 17 through the pipeline, burn out the combustible gas replaced in the secondary combustion chamber 17, the solid replaced in returning charge ash replaces storehouse 23 is connected to the vibrating screen 31 through the conveying appliance; the ash recovery device of the secondary combustion chamber comprises an ash bucket 19 and an ash bin 20 which are arranged at the bottom of the secondary combustion chamber, and an outlet of the ash bin is connected with a vibrating screen 31 of the feeding system through a conveying device.
Example 2
The embodiment discloses a method for gasifying and incinerating high-nitrogen high-sulfur gelatinous asphaltene dangerous waste by using the device in the embodiment 1:
(1) The bed material (3 mm+/-1 mm quartz sand) is sieved by a vibrating screen 31, large particles are sequentially thrown into a gasification furnace 9 through a bucket elevator 1, a bed material storage bin 3, a screw conveyor 4 and a bed material feeding pipe 5, and fall on an air distribution plate 32, high-nitrogen high-sulfur colloid asphaltene dangerous waste is changed into a liquid form with good fluidity after being subjected to steam tracing treatment in a conveying pipeline, is conveyed to an inlet of an atomization spray gun 6 through a booster pump 2, liquid dangerous waste is sprayed into the gasification furnace 9 under the action of compressed air serving as an atomization medium, high-pressure air is introduced into the gasification furnace 9 through a Roots blower 8, the amount of the introduced high-pressure air is 0.3 times of the amount of air required for completely burning the dangerous waste, a hypoxia environment is formed, the high-pressure air enables the dangerous waste and the bed material to be fluidized and mixed in the gasification furnace 9, part of the dangerous waste is burnt in the environment of high-pressure fluidization wind, oxygen in the high-pressure fluidization wind is completely consumed, a large amount of heat is released, energy is provided for the gasification of the other part of dangerous waste, and C, H, O, N and S is converted into a small amount of combustible organic gas such as N 2、H2S、CO、CO2 and SO 2、H2 in the gasification process; in the process, the Roots blower 8 is controlled to control the air quantity fed into the gasifier, and the temperature in the gasifier is controlled to be 650-850 ℃.
(2) The organic combustible gas, the thermal state bed material and solid carbon, tar and other substances generated by incomplete gasification enter a cyclone separator 10 through an upper outlet flue of a gasification furnace 9 for gas-solid separation, the separated thermal state bed material and solid carbon, tar and other substances generated by incomplete gasification enter a material returning device 12 through a dipleg 11 positioned at the lower part of the cyclone separator 10, the solid materials in the dipleg 11 are loosened through loose air, then high-pressure N 2 is introduced into the material returning device 12 as feeding air to return the solid materials entering the material returning device 12 into the gasification furnace 9, the cyclone separator 10 and the material returning device 12 form a gasification mode of a circulating fluidized bed, and the loose air and the feeding air are high-pressure inert gases;
(3) The organic combustible gas separated by the cyclone separator 10 is conveyed to the secondary combustion chamber 17 through a flue, combustion air is fed into the secondary combustion chamber 17 through a secondary combustion chamber blower 15, so that the organic combustible gas is combusted in the secondary combustion chamber 17, high-temperature flue gas after combustion is discharged from a flue gas outlet 18 of the secondary combustion chamber, the flow rate of the blown combustion air is controlled in the process, and the dry oxygen content in the combusted flue gas is 6% -10% through an oxygen meter arranged at the flue gas outlet 18 of the secondary combustion chamber in real time, so that the organic combustible gas is ensured to be fully combusted in the secondary combustion chamber 17;
(4) When ash is required to be removed, the ash discharging valve 26 of the gasifier is closed, N 2 gas is introduced into the ash replacing bin 28 of the gasifier, organic combustible gas carried by ash in the ash replacing bin 28 of the gasifier is carried out by N 2, the organic combustible gas is discharged and conveyed to the secondary combustion chamber 17, and solids are conveyed to the vibrating screen 31 and mixed with the bed material for feeding; the ash and the bed material in the material returning device are treated in the same way as the ash and the bed material in the gasification furnace; ash in the secondary combustion chamber 17 falls into the secondary combustion chamber ash bin 20 from the secondary combustion chamber ash hopper 19 positioned at the bottom of the secondary combustion chamber 17 and is conveyed to the vibrating screen 31.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention, and not for limiting the same; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the invention.
Claims (10)
1. The high-nitrogen high-sulfur gelatinous asphaltene dangerous waste gasification incineration system is characterized by comprising a feeding system, a gasification system, an incineration system and an ash collection system;
The feeding system comprises a bed material feeding device and a hazardous waste feeding device, wherein the bed material feeding device comprises a vibrating screen, a bed material storage bin and a bed material feeding pipe, and the hazardous waste feeding device comprises a booster pump, an atomizing spray gun and a conveying pipeline connected with the booster pump and the atomizing spray gun, and the conveying pipeline is used for laying a steam tracing pipeline along the path;
The gasification system comprises a gasification furnace, a cyclone separator and a material returning device, wherein an atomization spray gun and a bed material feeding pipe of the material feeding system are respectively connected to respective inlets of the gasification furnace, a wind distribution plate is arranged at the bottom of the gasification furnace, a wind distribution chamber is separated from the gasification chamber through the wind distribution plate, the inlet of the atomization spray gun is arranged on the gasification chamber, the inlet of the bed material feeding pipe is arranged above the wind distribution plate, a wind cap is arranged on the wind distribution plate to communicate the wind distribution chamber with the gasification chamber, one end of the wind distribution chamber is connected with one end of a furnace starting burner of the gasification furnace, the other end of the furnace starting burner is connected with a natural gas or light diesel fuel interface and a fluidized wind distribution interface, an outlet at the upper part of the gasification chamber of the gasification furnace is connected with the cyclone separator through a flue, solid materials separated by the cyclone separator enter a material returning device connected with a material leg, an outlet of the material returning device is connected to the gasification chamber of the gasification furnace, a wind cap and the wind distribution plate are also arranged in the material returning device, high-pressure inert gas is adopted to perform material loosening and feeding on the solid materials entering the material returning device through the wind cap, and the material returning device is fed into the gasification chamber;
The incineration system comprises a secondary combustion chamber connected with a combustible gas outlet flue generated by gasification of gas-solid separation of the cyclone separator, the secondary combustion chamber is also connected with a secondary combustion chamber blower through a gas distribution pipeline, a combustor is arranged at an inlet of the secondary combustion chamber, a flue gas outlet is arranged at the lower part of the secondary combustion chamber, and a secondary combustion chamber ash bucket and a secondary combustion chamber ash bin are sequentially arranged at the bottom of the secondary combustion chamber;
The ash collection system comprises a gasifier ash and slag recovery device, a returning charge ash recovery device and a secondary combustion chamber ash recovery device, wherein the gasifier ash and slag recovery device comprises a gasifier ash discharge pipe connected with an ash outlet at the bottom of the gasifier, the gasifier ash discharge pipe is connected with a gasifier ash replacement bin through a gasifier ash discharge valve, the gasifier ash replacement bin is provided with an inert gas inlet for replacing combustible gas in gasifier ash and a replaced combustible gas outlet, the combustible gas outlet is connected to the secondary combustion chamber through a pipeline, the replaced combustible gas is incinerated in the secondary combustion chamber, and solids replaced in the gasifier ash replacement bin are connected to a vibrating screen through a conveying device; the ash recovery device of the material returning device comprises an ash discharging pipe of the material returning device, which is connected with an ash discharging valve of the material returning device, and is connected with an ash replacing bin of the material returning device, wherein the ash replacing bin of the material returning device is provided with an inlet of inert gas for replacing combustible gas in ash of the ash replacing bin of the material returning device and an outlet of replaced combustible gas, the outlet of the combustible gas is connected to a secondary combustion chamber through a pipeline, the replaced combustible gas in the secondary combustion chamber is incinerated, and solids replaced in the ash replacing bin of the material returning device are connected to a vibrating screen through a conveying device; the ash recovery device of the secondary combustion chamber comprises an ash bucket and an ash bin which are arranged at the bottom of the secondary combustion chamber, and an outlet of the ash bin is connected with a vibrating screen through a conveying device.
2. The high nitrogen and sulfur gelatinous asphaltene hazardous waste gasification incineration system according to claim 1, wherein one or more steam injection ports are arranged in a dense phase zone at the lower part of the gasification furnace, and a gasification gas temperature measuring point is arranged at an outlet at the upper part of a gasification chamber of the gasification furnace.
3. The high nitrogen and sulfur gelatinous asphaltene hazardous waste gasification incineration system according to claim 1, wherein a flue gas temperature measuring point is arranged at a flue gas outlet at the lower part of the secondary combustion chamber.
4. The high nitrogen high sulfur gelatinous asphaltene hazardous waste gasification incineration system according to claim 1, wherein the bed material feeding device further comprises a bucket elevator connected between the vibrating screen and the bed material storage bin, and a screw conveyor connected between the bed material storage bin and the bed material feeding pipe.
5. A method for gasifying and incinerating high nitrogen and high sulfur colloidal asphaltene hazardous waste by using the system of claim 1, which comprises the following steps:
The bed material is put into a gasification furnace through a bed material feeding device, high-nitrogen high-sulfur gelatinous asphaltene dangerous waste is changed into a liquid form with good fluidity after being subjected to steam tracing treatment in a conveying pipeline, the liquid dangerous waste is conveyed to an inlet of an atomization spray gun through a booster pump, the liquid dangerous waste is sprayed into the gasification furnace after being atomized, high-pressure air is introduced into the gasification furnace through a Roots blower of the gasification furnace, the amount of the introduced high-pressure air is 0.2-0.35 times of the air amount required by complete combustion of the dangerous waste, a hypoxia environment is formed, the high-pressure air enables the dangerous waste and the bed material to be fluidized and mixed in the gasification furnace, a part of the dangerous waste is combusted in the environment of high-pressure fluidization wind, oxygen in the high-pressure fluidization wind is completely consumed, a large amount of heat is discharged, energy is provided for gasification of another part of dangerous waste, and C, H, O, N and S in the dangerous waste are converted into N 2、H2S、CO、CO2, a small amount of SO 2、H2 and other mixed organic combustible gases in the gasification process;
The organic combustible gas, the thermal-state bed material, solid carbon, tar and other substances generated by incomplete gasification enter a cyclone separator connected with the gasification furnace through an outlet flue at the upper part of the gasification furnace, gas-solid separation is carried out on the combustible gas generated by gasification, the separated solid materials enter a material returning device connected with a material leg through a material leg at the lower part of the cyclone separator, the solid materials of the material leg are loosened through loose air, and the solid materials entering the material returning device are returned to the gasification furnace through feeding air to carry out gasification reaction again, so that the gasification furnace, the cyclone separator and the material returning device form a gasification mode of a circulating fluidized bed; the loosening air and the feeding air are high-pressure inert gases;
The organic combustible gas separated by the cyclone separator is conveyed to a secondary combustion chamber through a flue, combustion air is fed into the secondary combustion chamber through a secondary combustion chamber blower, so that the organic combustible gas is combusted in the secondary combustion chamber, and high-temperature flue gas after combustion is discharged from a flue gas outlet of the secondary combustion chamber;
When ash is needed to be removed, the ash discharging valve of the gasifier is closed, inert gas is introduced into the ash replacing bin of the gasifier, organic combustible gas carried in ash in the ash replacing bin of the gasifier is replaced by the inert gas, the organic combustible gas is replaced and discharged and conveyed to a secondary combustion chamber, the secondary combustion chamber is burnt, and solids are conveyed to a vibrating screen through a conveying device; the ash and the bed material in the material returning device are treated in the same way as the ash and the bed material in the gasification furnace; ash in the secondary combustion chamber falls into the ash bin of the secondary combustion chamber from the ash hopper of the secondary combustion chamber positioned at the bottom of the secondary combustion chamber, and is then conveyed to the vibrating screen through the conveying device.
6. The method of claim 5, wherein the atomizing is atomizing with low pressure steam or compressed air as an atomizing medium or directly with pressure without an atomizing medium.
7. The method according to claim 5, wherein the auxiliary fuel is supplied by the combustion of the burner of the gasifier when the gasifier is started, and the feeding operation is started after the temperature in the gasifier is raised to 650-850 ℃.
8. The method according to claim 5, wherein the organic combustible gas is combusted in the secondary combustion chamber, the dry oxygen content in the combusted flue gas is 6% -10% by controlling the flow of the blown combustion air, so that the organic combustible gas is ensured to be fully combusted in the secondary combustion chamber, the burner acts as a pilot lamp, the combustion is ensured to be safe and reliable, the secondary combustion chamber burner is started when the temperature of the flue gas at the outlet of the secondary combustion chamber is lower than 1100 ℃, the condition requirement that the temperature of the flue gas at the outlet of the secondary combustion chamber is more than or equal to 1100 ℃ is met, and the requirement of the sufficient environmental protection standard is ensured to be met.
9. The method according to claim 5, wherein the organic combustible gas discharged from the gasifier ash replacement bin and the return ash replacement bin is also transported to the secondary combustion chamber for incineration through a pipeline.
10. The method of claim 5, further comprising the step of sending the flue gas to a lower grade tail gas environmental treatment system and a sulfur or sulfuric acid recovery system for tail gas treatment.
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