CN214426014U - High-nitrogen high-sulfur colloidal asphaltene dangerous waste gas incineration system - Google Patents
High-nitrogen high-sulfur colloidal asphaltene dangerous waste gas incineration system Download PDFInfo
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Abstract
The utility model provides a high nitrogen high sulphur colloidal asphaltene danger exhaust gas ization system of burning, including throwing the material system, gasification system, burn the system, lime-ash collecting system, the utility model discloses a bed material participates in the gasification to become useless heating of danger and spout into the gasifier with the atomizing mode after the liquid form, gasification system passes through the gasifier, the connected mode between cyclone and the returning charge ware forms circulating fluidized bed's gasification mode, makes the useless organic matter part of burning of danger provide the energy for the gasification schizolysis, and the useless gasification schizolysis under the high temperature state of mixing together through the fluidization wind with the bed material of danger generates organic combustible gas, the gasification in-process not complete gasification and the solid carbon that produces, material such as tar. Solves the technical problems that the high-nitrogen high-sulfur colloidal asphaltene hazardous waste in the prior art is extremely high in nitrogen oxide generated by incineration, is easy to generate deflagration in combustion, is overhigh in natural gas consumption of a secondary combustion chamber, and can separate out organic carbon black which is difficult to burn out by incineration and the like.
Description
Technical Field
The utility model relates to a chemical industry danger is useless burns environmental protection processing technology, especially relates to a high-nitrogen high-sulfur colloidal asphaltene danger gasification system of burning, belongs to energy-concerving and environment-protective field.
Background
At present, one or more high-nitrogen high-sulfur normal-temperature solid and heated liquid high-viscosity hazardous wastes generated in the production process of chemical industry, rubber, petroleum refining, petrochemical industry, medicine manufacturing, coating, printing ink, plastic product manufacturing and other industries in China have the characteristics of high heat value, high nitrogen content, high sulfur content, normal-temperature solid crushing, explosion liability, poor liquid high-viscosity fluidity and the like, have the dangerous characteristics of flammability, explosion liability, toxicity, harm and the like, and easily precipitate carbon black during combustion, thus belonging to the hazardous wastes.
The method for treating the waste in China generally adopts an incineration mode, wherein a fixed hearth furnace is adopted for incineration, a chamber furnace is adopted for incineration, a rotary kiln is adopted for adding a secondary combustion chamber, a fluidized bed or a circulating fluidized bed is adopted for incineration, the method basically cannot run reliably, and the problems of difficult feeding and feeding, large amount of carbon black precipitation, deflagration, high generation amount of smoke nitrogen oxides, serious equipment corrosion and the like exist. No method or means for effective incineration disposal has been found to date.
The problems mainly existing in the incineration process of treating the high-nitrogen high-sulfur normal-temperature solid, heated liquid and high-viscosity dangerous wastes in the existing stage of incineration mode are summarized as the following points:
(1) most of the wastes are solid at normal temperature, become soft and sticky when heated to about 30-40 ℃, exist in sticky states such as paste and asphalt when the temperature is above 60 ℃, and cannot be crushed at normal temperature or after being frozen because the wastes have high sulfur content and high heat value and have explosion danger during crushing.
(2) The waste heating temperature is low, the fluidity is poor, the viscosity is high, the fluidity is good when the heating temperature is high, but the waste heating temperature is easy to crack to generate combustible gas, the waste heating temperature is very difficult to enter a furnace and atomize, and the problems that an inlet pipe (opening) and an atomizing spray gun are blocked, the atomizing quality is poor and the like are easily caused.
(3) The waste has high nitrogen content and high heat value, the combustion temperature is very high during burning, the generation amount of fuel type and thermal type nitrogen oxides is very high, and the investment cost and the operation cost of a rear-stage denitration device are increased.
(4) The waste is high in sulfur content, and the waste needs to react under the conditions of oxygen enrichment and high temperature during incineration to convert the sulfur in the waste into sulfur dioxide; and sulfur dioxide reacts with the ammonia gas that the denitration reductant of spouting produced in subsequent denitration treatment process and forms ammonium sulfate salt, can produce very big influence: A. sulfur dioxide corrodes the SCR denitration catalyst to make the SCR denitration catalyst lose activity; B. ammonium sulfate is attached to the surface of the denitration catalyst to block the SCR denitration catalyst from contacting with flue gas, so that the denitration catalyst loses activity; C. the ammonium sulfate salt not only blocks a flue gas channel of the denitration catalyst, but also blocks flue gas channels of other equipment, so that the stable operation of the system is influenced, and a certain amount of ammonium sulfate salt which is a flammable and combustible chemical is accumulated in the system and can cause explosion at a certain temperature; D. after being discharged and collected, ammonium sulfate is new dangerous waste, causes secondary pollution and needs secondary environmental protection treatment.
(5) Sulfur dioxide, nitrogen oxide content are higher in the flue gas that produces behind this kind of waste incineration, if will carry out sulphur and retrieve or sulphuric acid and retrieve, will lead to containing the ammonium sulfate salt that nitric acid and denitration in-process generated in the sulphur of retrieving, the sulphuric acid or sulphur by-product purity seriously influence, probably cause the condition that can't sell or recycle even, need reprocess, cause the secondary burden for the enterprise.
(6) This type of wastes material is macromolecular structure usually, and C atomic content is higher (be more than C8 usually), gets into after the incinerator because of being heated, the volume can expand fast, and becomes thick and thick form, pastes full incinerator, causes to burn the air distribution confusion, appears the burner, and some local oxygen boosting, some local lack oxygen consequently can precipitate a large amount of carbon black, tar particle class material and CO, CH that do not burn to the utmost, can separate out4And combustible gas enters subsequent equipment, so that the smoke is difficult to discharge after reaching the environmental protection standard.
Disclosure of Invention
To the useless problem that is difficult to handle and incineration disposal is not good of above-mentioned high nitrogen high sulphur gelatineous asphaltene danger, the utility model provides a high nitrogen high sulphur gelatineous asphaltene danger system of burning to it is useless to realize that effective, reliable method carries out environmental protection, harmless, this type of high nitrogen high sulphur gelatineous asphaltene danger of resourceful treatment.
In order to achieve the above object, the utility model adopts the following technical scheme:
the utility model provides a high-nitrogen high-sulfur colloidal asphaltene hazardous waste gas incineration system, which comprises a feeding system, a gasification system, an incineration system and an ash residue 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, 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 a steam heat tracing pipeline is laid along the conveying pipeline;
the gasification system comprises a gasification furnace, a cyclone separator and a material returning device, an atomization spray gun and a bed material feeding pipe of the feeding system are respectively connected to respective inlets of the gasification furnace, an air distribution plate is arranged at the bottom in the gasification furnace, an air distribution chamber is separated from a gasification reaction chamber through the air 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 air distribution plate, an air cap is arranged on the air distribution plate to communicate the air distribution chamber with the gasification chamber, one end of the air distribution chamber is connected with one end of a gasification furnace start-up burner, the other end of the gasification furnace start-up burner is connected with a natural gas or light diesel fuel interface and a fluidized air 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 the material returning device connected with a dipleg through dipleg, and an outlet of the material returning device is connected to the gasification chamber of the gasification furnace, the return feeder is also internally provided with a hood and an air distribution plate, high-pressure inert gas is adopted to loosen and feed solid materials entering the return feeder through the hood, the loose materials aim at leg materials of the cyclone separator, and the feeding is to send the materials in the return feeder into a gasification chamber of the gasification furnace;
the incineration system comprises a secondary combustion chamber connected with a combustible gas outlet flue generated by gasification of gas-solid separation of a cyclone separator, the secondary combustion chamber is also connected with a secondary combustion chamber blower through a gas distribution pipeline, a burner is arranged at the 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 hopper and a secondary combustion chamber ash bin are sequentially arranged at the bottom of the secondary combustion chamber;
the ash collecting system comprises a gasifier ash recovery device, a return feeder ash recovery device and a secondary combustion chamber ash recovery device, wherein the gasifier ash recovery device comprises a gasifier ash discharge pipe connected with an ash outlet at the bottom of a 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 the gasifier ash and an outlet for replaced combustible gas, the outlet for the combustible gas is connected to the secondary combustion chamber through a pipeline, the replaced combustible gas is burnt in the secondary combustion chamber, and solid replaced in the gasifier ash replacement bin is connected to a vibrating screen through a conveying device; the ash recovery device of the return feeder comprises a return feeder ash discharge pipe connected with an ash outlet at the bottom of the return feeder, the return feeder ash discharge pipe is connected with a return feeder ash displacement bin through a return feeder ash discharge valve, the return feeder ash displacement bin is provided with an inert gas inlet for displacing combustible gas in ash in the return feeder ash displacement bin and a displaced combustible gas outlet, the combustible gas outlet is connected to a secondary combustion chamber through a pipeline, the displaced combustible gas is incinerated in the secondary combustion chamber, and the displaced solid in the return feeder ash displacement bin is connected to a vibrating screen through a conveying device; the ash recovery device of the secondary combustion chamber comprises an ash hopper 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 the vibrating screen through a conveying device.
Furthermore, one or more steam injection ports are arranged in a dense-phase region at the lower part of the gasification furnace, a gasified gas temperature measuring point is arranged at an outlet at the upper part of the gasification chamber of the gasification furnace, steam can be sprayed into the gasification furnace according to the gasified gas temperature measured by the gasified gas temperature measuring point and the air distribution quantity of the gasification furnace so as to control the temperature of the gasification furnace, and simultaneously, the injection of the steam is favorable for gasification reaction, so that H, O is provided for the gasification reaction to generate CH4、CO、 H2S；
Further, a smoke temperature measuring point is arranged at a smoke outlet at the lower part of the secondary combustion chamber, air can be supplied 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 supply, a secondary combustion chamber burner containing an 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 organic components in gasified gas are completely burnt;
further, the bed material feeding device also comprises a necessary material conveying device, 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.
Furthermore, a fluidization air cap is arranged on an air distribution plate in the gasification furnace, and air distribution in an air distribution chamber is guided into the gasification reaction chamber for gasification reaction.
Furthermore, the air volume and the air pressure of the Roots blower are controlled according to the temperature in the gasifier.
Furthermore, the second combustion chamber is also provided with safety devices such as an explosion door and the like. In addition, in order to ensure safety, the burner is a pilot burner.
The combustor of the secondary combustion chamber is a combustor for burning natural gas or light diesel oil.
In addition, the utility model also discloses a method for utilizing above-mentioned system to carry out gasification incineration to high nitrogen high sulfur colloidal asphaltene danger is useless, including following content:
the bed material is thrown into the gasifier through a bed material feeding device, high-nitrogen high-sulfur colloidal asphaltene hazardous waste is subjected to steam heat tracing treatment in a conveying pipeline and is changed into a liquid form with good fluidity, the high-nitrogen high-sulfur colloidal asphaltene hazardous waste is conveyed to an inlet of an atomizing spray gun through a booster pump and is sprayed into the gasifier after being atomized, high-pressure air is introduced into the gasifier through a Roots blower of the gasifier, the amount of the introduced high-pressure air is 0.2-0.35 times of the air amount required by complete combustion of the hazardous waste, an oxygen-deficient environment is formed, the hazardous waste and the bed material are fluidized and mixed in the gasifier through the high-pressure air, part of the hazardous waste is combusted under the environment of high-pressure fluidized air, oxygen in the high-pressure fluidized air is completely consumed, a large amount of heat is discharged, energy is provided for gasification of the other part of the hazardous waste, and C, H, O, N and S in the hazardous waste are converted into N in the gasification process2、H2S、CO、CO2And a small amount of SO2、H2Mixing the organic combustible gas;
the organic combustible gas, the hot bed material and solid carbon, tar and other substances generated by incomplete gasification enter a cyclone separator connected with the gasification furnace through an upper outlet flue of the gasification furnace, the combustible gas generated by gasification is subjected to gas-solid separation, the separated solid material enters a material returning device connected with a material leg through the material leg at the lower part of the cyclone separator, the solid material of the material leg is loosened through material loosening wind, the solid material entering the material returning device is returned to the gasification furnace through material conveying wind, gasification reaction is carried out again, and the gasification furnace, the cyclone separator and the material returning device form a gasification mode of a circulating fluidized bed; both 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-supporting air is fed into the secondary combustion chamber through a secondary combustion chamber blower, 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;
ash and bed materials in the gasification furnace fall into an ash replacement bin of the gasification furnace through an ash discharge pipe of the gasification furnace positioned at the bottom of the gasification furnace, when ash removal is needed, an ash discharge valve of the gasification furnace is closed, inert gas is introduced into the ash replacement bin of the gasification furnace, organic combustible gas carried in the ash replacement bin of the gasification furnace is replaced and taken out by the inert gas, the replaced and discharged organic combustible gas is conveyed to a secondary combustion chamber and incinerated, and solids are conveyed to a vibrating screen through a conveying device; ash and bed materials in the material returning device are treated in the same way as the ash and bed materials in the gasification furnace; the ash in the secondary combustion chamber falls into a secondary combustion chamber ash bin from a secondary combustion chamber ash hopper positioned at the bottom of the secondary combustion chamber, and then is conveyed to a vibrating screen through a conveying device.
Further, the bed material adopts quartz sand with the thickness of 3mm +/-1 mm.
Further, the atomization is that low-pressure steam or compressed air is adopted as atomization medium or pressure atomization without atomization medium is directly adopted.
Further, when a furnace starting burner of the gasification furnace is used for baking the furnace and starting the furnace, bed materials on an air distribution plate in the gasification furnace are heated by burning natural gas or light diesel oil, and when the bed materials are heated to above 650 ℃, feeding operation is started. The burner of the gasification furnace burns auxiliary fuel to provide energy to heat the bed material to about 650-850 ℃ when the furnace is started and is baked newly, and then the feeding operation is started.
Furthermore, the gasification temperature of the gasification furnace is controlled to be about 850 ℃, the temperature is controlled mainly by controlling the air volume and the air pressure of the Roots blower and the steam sprayed into the gasification furnace, the temperature in the gasification furnace can be increased by increasing the air volume and the air pressure, and the temperature in the gasification furnace can be reduced by spraying the steam.
Furthermore, an oxygen meter is arranged at a flue gas outlet of the secondary combustion chamber, organic combustible gas generated by the gasification furnace is combusted in the secondary combustion chamber, the flow of blown combustion air is adjusted by controlling the opening degree of an air adjusting door of an air distribution blower of the secondary combustion chamber according to the measured value of the oxygen meter at the flue gas outlet of the secondary combustion chamber, so that the dry oxygen content in the combusted flue gas is ensured to be 6-10 percent, the organic combustible gas generated by the gasification furnace is ensured to be fully combusted in the secondary combustion chamber, the combustor acts as a pilot burner, the combustion is ensured to be safe and reliable, the combustor of the secondary combustion chamber is opened 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 not lower than 1100 ℃ is met, and the requirement of full combustion environmental protection standard is met.
And further, the organic combustible gas discharged from the gasification furnace ash replacement bin and the material returning device ash replacement bin is conveyed to a second combustion chamber through a pipeline for incineration.
Further, the gas introduced into the return feeder, the gasifier ash replacement bin and the return feeder ash replacement bin is inert gas, preferably N2。
And further, the method also comprises the step of sending the flue gas generated after the secondary combustion chamber is incinerated into a lower-level tail gas environment-friendly treatment system and a sulfur or sulfuric acid recovery system for tail gas treatment.
The utility model discloses a colloidal asphaltene danger of high nitrogen high sulfur system of burning compares with prior art and has following advantage:
(1) the system adopts a method of gasifying the high-nitrogen high-sulfur colloidal asphaltene hazardous waste and then burning combustible gas generated by gasification to treat the high-nitrogen high-sulfur colloidal asphaltene hazardous waste, so that organic nitrogen in the chemical hazardous waste is converted into N2The formation of fuel-type nitrogen oxides during combustion is reduced. If the waste is directly combusted, the formation amount of the nitrogen oxides converted from organic nitrogen in the high-nitrogen high-sulfur colloidal asphaltene hazardous waste is huge, the post-stage environmental protection treatment is difficult, and the waste is difficult to reach the standard and discharge. Meanwhile, because the gasification adopts hypoxic incineration, part of the organic matters are incinerated to provide energy for gasification, mainly organic combustible gas is generated, and the high-sulfur organic matters are converted into H in the gasification process2S is dominant and produces a small amount of SO2Thus, corrosion of the gasification system is reduced.
(2) The system adopts the method of firstly gasifying the high-nitrogen high-sulfur colloidal asphaltene hazardous waste and then burning the combustible gas generated by gasification to treat the high-nitrogen high-sulfur colloidal asphaltene hazardous waste, so that the secondary combustion requirement for a large amount of auxiliary fuel is reduced, and the operation cost for treating the high-nitrogen high-sulfur colloidal asphaltene chemical hazardous waste is reduced.
(3) This system is because adopting circulating fluidized bed gasifier to high nitrogen high sulphur colloidal asphaltene danger useless gasify, can effectively eliminate the useless carbon black of high nitrogen high sulphur colloidal asphaltene danger and separate out. If high-nitrogen high-sulfur colloidal asphaltene hazardous waste with high calorific value is directly combusted, a large amount of carbon black is separated out, the Ringelmann blackness of the discharged flue gas is increased and does not reach the standard, the carbon black which is not completely combusted causes energy waste, meanwhile, the separated carbon black is fine particles, the fine particles have the effects of static electricity, Van der Waals force, force among molecules and the like, the large amount of carbon black is easy to deposit in a system flue gas flow passage, the danger of explosion of the system and the flue gas flow passage 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 reduced, 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 adopts the mode that the high-nitrogen high-sulfur colloidal asphaltene hazardous waste is in a liquid state through steam tracing and is sprayed into the gasification furnace through atomization to carry out gasification reaction, and the atomized chemical hazardous waste is small in particle size and is in dispersed fluidization to be mixed with hot bed materials, so that the high gasification reaction rate is ensured, the chemical hazardous waste organic matter is completely and thoroughly treated, and the incineration rate is high.
(5) The system adopts the circulating fluidized bed and the bed materials to participate in gasification, so that the chemical hazardous wastes sprayed into the gasification furnace can be fully mixed with the hot bed materials, the hot bed materials and the chemical hazardous wastes are in a circulating fluidized reaction process of suspension, cross collision and the like in the whole system, and the gasification efficiency of the chemical hazardous wastes is increased. Meanwhile, in the system and the method, substances such as solid carbon, tar and precipitated carbon black generated by incomplete gasification of macromolecular substances in hazardous wastes are fully mixed with bed materials in the gasification process, the combustible gas generated by gasification is subjected to gas-solid separation by a gas-solid separator, the separated substances such as the solid carbon, the tar and the precipitated carbon black return to the circulating fluidized bed gasification furnace through a return feeder, the gasification furnace is carried out again, and the process is repeated, so that organic substances in chemical hazardous wastes are gasified more thoroughly, and the complete gasification and incineration of the organic substances in the chemical hazardous wastes are ensured.
(6) The gasification process in the system converts nitrogen into nitrogen instead of nitrogen oxide under the conditions of low temperature and insufficient oxygen, ensures that the content of the nitrogen oxide 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 process of the system.
(7) The system can utilize the circulating bed materials to provide gasification preheating energy for the waste newly entering the furnace, thereby reducing the waste amount needing to be incinerated, namely reducing the conveying amount of air, namely: the amount of nitrogen oxides generated can be further reduced, and the running cost can be reduced.
(8) The tail gas finally discharged in the system has low content of nitrogen oxides and high content of sulfur dioxide, so the tail gas can be completely sent to a subsequent system for sulfur recovery or sulfuric acid recovery treatment, and the problem of influencing the purity of sulfur or sulfuric acid as described in the background technology does not exist.
(9) The ash in the system is recycled, no waste water is discharged, and the generated high-temperature flue gas is sent into 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 utility project in this system only consumes the atomizing medium that is a small amount of wastes material and the electricity that the fan consumed, and the running cost is extremely low to exhaust tail gas accessible follow-up system carries out waste heat recovery and sulphur recovery or is sulphuric acid recovery, has realized that low investment cost, low running cost handle high nitrogen high sulphur colloidal asphalt class chemical industry danger useless and the by-product steam and sulphur or sulphuric acid, has not only disposed hazardous waste for the enterprise but also created economic benefits for the enterprise.
Drawings
FIG. 1 is a high nitrogen high sulfur colloidal asphaltene hazardous waste gas incineration system of example 1;
FIG. 2 is a schematic view showing the structure of a gasification chamber and an 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 burner of the gasification furnace; 8. a 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 second combustion chamber burner containing a pilot burner; 15. a second combustion chamber blower; 16. an explosion vent; 17. a second combustion chamber; 18. A flue gas outlet; 19. a second combustion chamber ash hopper; 20. a second combustion chamber ash bin; 21. ash discharge pipes of the material returning device; 22. a material returning device ash discharging valve; 23. a return feeder ash residue replacement bin; 24. an inert gas inlet for replacing combustible gas in the return feeder ash replacement bin ash; 25. a combustible gas outlet displaced by the ash displacement bin of the return feeder; 26. a gasification furnace ash discharge pipe; 27. a gasification furnace ash discharge valve; 28. a gasification furnace ash residue replacement bin; 29. an inlet for an inert gas for replacing the combustible gas in the gasification furnace ash; 30. a combustible gas outlet displaced by the gasification furnace ash displacement bin; 31. the device comprises a vibrating screen, a 32 air distribution plate, a 33 air distribution chamber, a 34 air cap, a 35 gasification chamber, a 36 fluidized air distribution interface, a 37 fluidized air distribution channel, a 38 fluidized air volume control air adjusting door, a 39 fuel interface such as natural gas or light diesel oil, a 40 material returning device outlet, a 41 steam injection port, a 42 gasified gas temperature measuring point, a 43 flue gas temperature measuring point.
Detailed Description
The invention is further illustrated below with reference to the following examples:
example 1
The embodiment discloses a high-nitrogen high-sulfur colloidal asphaltene dangerous waste gas gasification incineration system, which comprises a feeding system, a gasification system, an incineration system and an ash collecting system, as shown in fig. 1 and 2;
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, the hazardous waste feeding device comprises a booster pump 2, an atomizing spray gun 6 and a conveying pipeline connected with the two, and a steam heat tracing pipeline is laid along the conveying pipeline;
the gasification system comprises a gasification furnace 9, a cyclone separator 10 and a material returning device 12, and an atomization spray gun 6 and a bed material feeding pipe 5 of the feeding systemRespectively connected with the inlets of the gasification furnaces, an air distribution plate 32 is arranged at the bottom in the gasification furnace 9, an air distribution chamber 33 is separated from the gasification chamber 35 by the air distribution plate 32, the inlet of an atomizing spray gun is arranged on the gasification chamber 35, the inlet of a 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 gasification furnace start-up burner 7, the other end of the gasification furnace start-up burner 7 is connected with a natural gas or light diesel fuel interface 39 and a fluidizing air distribution interface 36, a fluidizing air quantity control air regulating door 38 is also arranged between the fluidizing air distribution interface 36 and a fluidizing air distribution channel 37, the upper outlet of the gasification chamber 35 of the gasification furnace is connected with a cyclone separator 10 by a flue, solid materials separated by the cyclone separator 10 enter a return feeder 12 connected with a dipleg 11 by a dipleg 11 at the lower part, the outlet 40 of the return feeder is connected to the gasification chamber 35 of the gasification furnace, the return feeder 12 is also provided with a blast cap and a wind distribution plate, high-pressure inert gas is adopted to loosen and feed the solid material entering the return feeder 12 through the blast cap, the loosened material is directed at the dipleg material of the cyclone separator 10, the material in the return feeder 12 is fed into the gasification chamber 35 of the gasification furnace, one or more steam injection ports 41 are arranged in the dense-phase region at the lower part of the gasification furnace, the upper outlet of the gasification chamber of the gasification furnace is provided with a gasification gas temperature measurement point 42, steam can be sprayed into the gasification furnace according to the gasification gas temperature measured by the gasification gas temperature measurement point 42 at the outlet of the gasification furnace and the air distribution quantity of the gasification furnace to control the temperature of the gasification furnace, meanwhile, the injection of the steam is favorable for gasification reaction, and H, O is provided for generating CH for the gasification reaction4、CO、H2S；
The incineration system comprises a secondary combustion chamber 17 connected with a combustible gas outlet flue 13 generated by the gasification of the gas-solid separation of the cyclone separator 10, the secondary combustion chamber 17 is also connected with a secondary combustion chamber air blower 15 through an air distribution pipeline, a secondary combustion chamber combustor 14 containing an incandescent lamp and a safety device such as an explosion door 16 are arranged at the inlet of the secondary combustion chamber, a smoke outlet 18 is arranged at the middle lower part of the secondary combustion chamber 17, a secondary combustion chamber ash hopper 19 and a secondary combustion chamber ash bin 20 are sequentially arranged at the bottom of the secondary combustion chamber 17, a flue gas temperature measuring point 43 is arranged at the flue gas outlet 14 at the lower part of the secondary combustion chamber, so that air can be supplied into the secondary combustion chamber according to the flue gas temperature measured by the flue gas temperature measuring point 43, the flue gas temperature is reduced when air is supplied, starting a second combustion chamber burner 14 containing an pilot burner to assist in burning natural gas or light diesel oil, so that the temperature of the flue gas measured by a flue gas temperature measuring point 43 is not lower than 1100 ℃, and organic components in the gasified gas are completely burnt;
the ash collecting system comprises a gasifier ash recovery device, a return feeder ash recovery device and a secondary combustion chamber ash recovery device, wherein the gasifier ash recovery device comprises a gasifier ash discharge pipe 26 connected with an ash outlet at the bottom of a gasifier, the gasifier ash discharge pipe is connected with a gasifier ash replacement bin 28 through a gasifier ash discharge valve 27, the gasifier ash replacement bin 28 is provided with an inert gas inlet 29 for replacing combustible gas in the gasifier ash and an combustible gas outlet 30 for replacing the combustible gas in the gasifier ash replacement bin, the inert gas outlet is connected to the secondary combustion chamber 17 through a pipeline, the replaced combustible gas is burnt in the secondary combustion chamber 17, and solid replaced in the gasifier ash replacement bin 28 is connected to a vibrating screen 31 through a conveying device; the ash recovery device of the return feeder comprises a return feeder ash discharge pipe 21 connected with an ash outlet at the bottom of the return feeder, the return feeder ash discharge pipe is connected with a return feeder ash replacement bin 23 through a return feeder ash discharge valve 22, the return feeder ash replacement bin 23 is provided with an inert gas inlet 24 for replacing combustible gas in the ash of the return feeder ash replacement bin and a combustible gas outlet 24 replaced by the return feeder ash replacement bin, the inert gas inlet 24 is connected with a secondary combustion chamber 17 through a pipeline, the replaced combustible gas is burned in the secondary combustion chamber 17, and the solid replaced in the return feeder ash replacement bin 23 is connected with a vibrating screen 31 through a conveying device; the ash recovery device of the secondary combustion chamber comprises an ash hopper 19 and an ash bin 20 which are arranged at the bottom of the secondary combustion chamber, and the outlet of the ash bin is connected with a vibrating screen 31 of a feeding system through a conveying device.
The process of gasification incineration of high nitrogen and high sulfur colloidal asphaltene hazardous waste using the apparatus of example 1 was as follows:
(1) the bed material (3mm +/-1 mm quartz sand) is screened to remove large particles through the vibrating screen 31, then is put into the gasification furnace 9 through the bucket elevator 1, the bed material storage bin 3, the screw conveyor 4 and the bed material feeding pipe 5 in sequence and falls on the air distribution plate 32, and the high-nitrogen high-sulfur colloidal asphaltene hazardous waste is in the conveying pipelineAfter the steam tracing heat treatment, the liquid state form with good fluidity is changed, the liquid state hazardous waste is conveyed to an inlet of an atomizing spray gun 6 through a booster pump 2, the liquid state hazardous waste is sprayed into a gasification furnace 9 under the action of compressed air serving as an atomizing 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 time of the amount of air required for the complete combustion of the hazardous waste, an oxygen-deficient environment is formed, the high-pressure air enables the hazardous waste and bed materials to be fluidized and mixed in the gasification furnace 9, part of the hazardous waste is combusted under the environment of high-pressure fluidized air, oxygen in the high-pressure fluidized air is completely consumed, a large amount of heat is released, energy is provided for the gasification of the other part of the hazardous waste, C, H, O, N and S in the hazardous waste are converted into N in the gasification process, and the N is added into the N2、H2S、CO、CO2And a small amount of SO2、H2Mixing the organic combustible gas; in the process, the air quantity sent into the gasification furnace is controlled by controlling the Roots blower 8, and the temperature in the gasification furnace is controlled to be 650-850 ℃.
(2) The organic combustible gas, the thermal state bed material and the 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 the 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 material in the dipleg 11 is loosened through material loosening wind, and high-pressure N is introduced into the material returning device 122The solid materials entering the material returning device 12 are sent back to the gasification furnace 9 as feeding air for gasification reaction again, 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 loosening air and the feeding air are both high-pressure inert gases;
(3) organic combustible gas separated by the cyclone separator 10 is conveyed to a secondary combustion chamber 17 through a flue, combustion-supporting air is fed into the secondary combustion chamber 17 through a secondary combustion chamber blower 15, 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, and in the process, the dry oxygen content in the flue gas after combustion is 6% -10% by controlling the flow of the blown combustion-supporting air and monitoring in real time through an oxygen meter arranged at the flue gas outlet 18 of the secondary combustion chamber, so that the organic combustible gas is ensured to be fully combusted in the secondary combustion chamber 17;
(4) the ash and bed materials in the gasification furnace 9 fall into an ash replacement bin 28 of the gasification furnace through a gasification furnace ash discharge pipe 26 positioned at the bottom of the gasification furnace, when ash removal is needed, the gasification furnace ash discharge valve 26 is closed, and N is introduced into the ash replacement bin 28 of the gasification furnace2Gas, organic combustible gas carried by ash in the gasifier ash displacement bin 28, N2Carrying out, discharging organic combustible gas, conveying the organic combustible gas to a secondary combustion chamber 17, conveying the solid to a vibrating screen 31, mixing the solid with bed materials and feeding the mixture; ash and bed materials in the material returning device are treated in the same way as the ash and bed materials in the gasification furnace; the ash in the second combustion chamber 17 falls into a second combustion chamber ash bin 20 from a second combustion chamber ash hopper 19 positioned at the bottom of the second combustion chamber 17 and is conveyed to a vibrating screen 31.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (8)
1. A high-nitrogen high-sulfur colloidal asphaltene dangerous waste gas gasification incineration system is characterized by comprising a feeding system, a gasification system, an incineration system and an ash residue 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, 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 a steam heat tracing pipeline is laid along the conveying pipeline;
the gasification system comprises a gasification furnace, a cyclone separator and a material returning device, an atomization spray gun and a bed material feeding pipe of the feeding system are respectively connected to respective inlets of the gasification furnace, an air distribution plate is arranged at the bottom in the gasification furnace, an air distribution chamber is separated from the gasification chamber through the air 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 air distribution plate, an air cap is arranged on the air distribution plate to communicate the air distribution chamber with the gasification chamber, one end of the air distribution chamber is connected with one end of a gasification furnace start-up burner, the other end of the gasification furnace start-up burner is connected with a natural gas or light diesel fuel interface and a fluidized air 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 the material returning device connected with a dipleg through dipleg, and an outlet of the material returning device is connected to the gasification chamber of the gasification furnace, the return feeder is also internally provided with a hood and an air distribution plate, high-pressure inert gas is adopted to loosen and feed solid materials entering the return feeder through the hood, the loose materials aim at leg materials of the cyclone separator, and the feeding is to send the materials in the return feeder into a gasification chamber of the gasification furnace;
the incineration system comprises a secondary combustion chamber connected with a combustible gas outlet flue generated by gasification of gas-solid separation of a cyclone separator, the secondary combustion chamber is also connected with a secondary combustion chamber blower through a gas distribution pipeline, a burner is arranged at the 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 hopper and a secondary combustion chamber ash bin are sequentially arranged at the bottom of the secondary combustion chamber;
the ash collecting system comprises a gasifier ash recovery device, a return feeder ash recovery device and a secondary combustion chamber ash recovery device, wherein the gasifier ash recovery device comprises a gasifier ash discharge pipe connected with an ash outlet at the bottom of a 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 the gasifier ash and an outlet for replaced combustible gas, the outlet for the combustible gas is connected to the secondary combustion chamber through a pipeline, the replaced combustible gas is burnt in the secondary combustion chamber, and solid replaced in the gasifier ash replacement bin is connected to a vibrating screen through a conveying device; the ash recovery device of the return feeder comprises a return feeder ash discharge pipe connected with an ash outlet at the bottom of the return feeder, the return feeder ash discharge pipe is connected with a return feeder ash displacement bin through a return feeder ash discharge valve, the return feeder ash displacement bin is provided with an inert gas inlet for displacing combustible gas in ash in the return feeder ash displacement bin and a displaced combustible gas outlet, the combustible gas outlet is connected to a secondary combustion chamber through a pipeline, the displaced combustible gas is incinerated in the secondary combustion chamber, and the displaced solid in the return feeder ash displacement bin is connected to a vibrating screen through a conveying device; the ash recovery device of the secondary combustion chamber comprises an ash hopper 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 the vibrating screen through a conveying device.
2. The hazardous waste gas incineration system of claim 1, wherein one or more steam injection ports are disposed in the lower dense phase zone of the gasifier.
3. The high-nitrogen high-sulfur colloidal asphaltene dangerous exhaust gas incineration system according to claim 1, characterized in that a gasification gas temperature measuring point is provided at an upper outlet of the gasification chamber of the gasification furnace.
4. The high-nitrogen high-sulfur colloidal asphaltene dangerous exhaust gas incineration system according to claim 1, characterized in that a flue gas temperature measuring point is provided at the flue gas outlet at the lower part of the secondary combustion chamber.
5. The system for incinerating dangerous exhaust gases containing high-nitrogen and high-sulfur colloidal asphaltenes as claimed in 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.
6. The system for incinerating the high-nitrogen high-sulfur colloidal asphaltene dangerous exhaust gas according to claim 1, wherein a hood arranged on a grid plate in the gasification furnace guides air in an air distribution chamber into the gasification reaction chamber for gasification reaction.
7. The high-nitrogen high-sulfur colloidal asphaltene dangerous exhaust gas incineration system according to claim 1, characterized in that the burner of the secondary combustion chamber is a natural gas or light diesel burner.
8. The high-nitrogen high-sulfur colloidal asphaltene dangerous exhaust gas incineration system according to claim 1, characterized in that the secondary combustion chamber is further provided with an explosion vent.
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| CN114087619A (en) * | 2021-11-12 | 2022-02-25 | 南京宇清环境科技有限公司 | Hazardous waste compatibility treatment process |
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