CN113970101A - Hazardous waste pyrolysis incineration system and temperature control method thereof - Google Patents

Hazardous waste pyrolysis incineration system and temperature control method thereof Download PDF

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CN113970101A
CN113970101A CN202010710904.9A CN202010710904A CN113970101A CN 113970101 A CN113970101 A CN 113970101A CN 202010710904 A CN202010710904 A CN 202010710904A CN 113970101 A CN113970101 A CN 113970101A
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kiln
pyrolysis
incineration
rotary kiln
air inlet
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CN113970101B (en
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李谦
周浩宇
叶恒棣
魏进超
沈维民
刘前
王业峰
陈思墨
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Zhongye Changtian International Engineering Co Ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/033—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment comminuting or crushing
    • 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
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2207/00—Control
    • F23G2207/10—Arrangement of sensing devices
    • F23G2207/101—Arrangement of sensing devices for temperature

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Incineration Of Waste (AREA)
  • Gasification And Melting Of Waste (AREA)

Abstract

The invention discloses a hazardous waste pyrolysis incineration system which comprises a pyrolysis rotary kiln and an incineration rotary kiln. And the discharge port of the pyrolysis rotary kiln is connected to the feed port of the incineration rotary kiln through a first pipeline. And the exhaust port of the pyrolysis rotary kiln is also connected to the air inlet channel of the incineration rotary kiln through a second pipeline. And the smoke outlet of the incineration rotary kiln is connected to the smoke inlet of the pyrolysis rotary kiln through a third pipeline. And a material inlet channel and an annular air inlet channel are arranged on the kiln head of the incineration rotary kiln. The system adopts the mode of multi-stage gas inlet and partition temperature detection of pyrolysis gas of the incineration rotary kiln, and adjusts the corresponding gas inlet amount change of each stage of gas inlet of the pyrolysis gas or adjusts the material input amount through the real-time temperature change. Thereby realizing the purposes of keeping the temperature in the incineration rotary kiln within the ideal incineration temperature range all the time, effectively preventing the ring formation phenomenon and reducing the generation of dioxin.

Description

Hazardous waste pyrolysis incineration system and temperature control method thereof
Technical Field
The invention relates to an incineration treatment system for organic hazardous waste pyrolysates, in particular to a hazardous waste pyrolysis incineration system and a temperature control method thereof, and belongs to the technical field of organic hazardous waste treatment.
Background
Generally, the incineration kiln can be used for incinerating organic hazardous wastes, is a rotary incineration kiln and is an important component device of a hazardous waste incineration system. The organic hazardous waste contains organic matters and has a certain calorific value, so that the organic hazardous waste is suitable for being treated in an incineration mode, the aim of reducing the volume of the hazardous waste can be achieved, the heat energy in the waste can be recovered, and the comprehensive utilization of resources is achieved.
The prior commonly-used hazardous waste rotary kiln is shown as figure 2, wherein a device 1 in the figure 2 is a rotary kiln head; the device 2 is a kiln body. The device 12 is a hazardous waste feed inlet; the device 13 is an air inlet; device 21 is a discharge outlet; in actual production, in order to make the material advance normally in the rotation process, the rotary kiln is installed with a certain inclination angle, which is higher at the left and lower at the right as shown in fig. 2.
The burning materials are pushed into the rotary kiln from the feeding hole of the device 12 by a hydraulic push rod (not shown in the figure), air enters the rotary kiln from the air inlet channel of the device 13, the materials are dried, pyrolyzed and ignited rapidly under the high-temperature environment, the burning materials are rolled continuously and move towards the tail of the kiln gradually under the rotation of the rotary kiln, the materials are combusted in the rolling and moving processes, and residues and smoke are discharged out of the kiln body from the discharging hole of the device 21.
In the prior art, a rotary kiln generally keeps a combustion temperature of 800-900 ℃, combustible components of hazardous wastes and air enter the rotary kiln from a kiln head, and after the hazardous wastes enter the rotary kiln, the hazardous wastes are rapidly dried, pyrolyzed and ignited and are fully contacted and combusted with the air under the rotation of the rotary kiln. However, the burning effect of the existing rotary kiln is not ideal, the temperature distribution along the kiln body direction is not uniform, the burning efficiency is not high, and the ring formation phenomenon easily occurs at the high-temperature section, which affects the normal production. It is also possible to increase the production of dioxins.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a separated type organic hazardous waste pyrolysis and incineration system, and the purposes of complete pyrolysis and thorough incineration of organic hazardous waste are realized by respectively carrying out anaerobic (or anoxic) pyrolysis and oxygen-enriched incineration on materials in two furnaces; meanwhile, combustible pyrolysis gas obtained by pyrolysis is used as incineration fuel, and high-temperature flue gas generated by incineration is used as a heat source in the pyrolysis process, so that comprehensive utilization of resources is realized. The invention also adopts the mode of multi-stage gas inlet and partition temperature detection of the pyrolysis gas of the incineration rotary kiln, and adjusts the corresponding gas inlet amount change of each stage of gas inlet of the pyrolysis gas or changes the material input amount through the real-time temperature change. Thereby realizing the purposes of keeping the temperature in the incineration rotary kiln within the ideal incineration temperature range all the time, effectively preventing the ring formation phenomenon and reducing the generation of dioxin.
In order to achieve the purpose, the technical scheme adopted by the invention is as follows:
according to a first embodiment of the invention, a hazardous waste pyrolysis incineration system is provided, and the system is a rotary kiln incineration system, and comprises a pyrolysis rotary kiln and an incineration rotary kiln. And the discharge port of the pyrolysis rotary kiln is connected to the feed port of the incineration rotary kiln through a first pipeline. And the exhaust port of the pyrolysis rotary kiln is also connected to the air inlet channel of the incineration rotary kiln through a second pipeline. And the smoke outlet of the incineration rotary kiln is connected to the smoke inlet of the pyrolysis rotary kiln through a third pipeline. Wherein, the burning rotary kiln comprises a kiln head, a kiln body and a burning discharge port. The kiln head is provided with a material inlet channel, a combustion air channel and an annular air inlet channel. The kiln body comprises a furnace lining and a hearth. And the material inlet channel and the combustion-supporting air channel penetrate through the kiln head and then are communicated to the hearth. The annular air inlet channel is arranged inside the kiln head. And a kiln body air inlet channel is also arranged in the furnace lining. One end of the kiln body air inlet channel is communicated with the annular air inlet channel. The other end of the kiln body air inlet channel is communicated with the hearth.
Preferably, the system also comprises a pyrolysis gas inlet pipeline and a heat supplementing fuel pipeline. The pyrolysis gas inlet pipeline and the heat supplementing fuel pipeline are both arranged on the kiln head. Wherein, pyrolysis gas inlet pipe is linked together with annular inlet channel. The heat supplementing fuel pipeline penetrates through the kiln head and is communicated with the hearth.
Preferably, the system further comprises an air inlet nozzle. And the air inlet nozzle is arranged in the hearth and is connected with an air outlet of the annular air inlet channel.
Preferably, the gas injection ports of the gas injection nozzles face the direction of the discharge port. Preferably, a separation net is arranged at the air injection port of the air inlet nozzle.
Preferably, the system also comprises a plurality of kiln body air inlet channels. And a plurality of kiln body air inlet channels are uniformly distributed in the furnace lining.
Preferably, the lengths of the kiln body air inlet channels in the direction from the kiln head to the kiln body are the same or different. Preferably, the lengths of the plurality of kiln body air inlet channels in the direction from the kiln head to the kiln body are sequentially increased.
Preferably, the number of the plurality of kiln body air inlet channels is 1-20, preferably 2-15, and more preferably 3-10.
Preferably, the system further comprises an inlet manifold valve. And the air inlet pipeline valve is arranged on the furnace lining corresponding to the air inlet channel of the kiln body. The opening degree of the kiln body air inlet channel is controlled by adjusting the air inlet pipeline valve. The number of the air inlet pipeline valves is consistent with that of the kiln body air inlet channels.
Preferably, the system further comprises a temperature probe. The temperature probe is arranged in the hearth.
Preferably, the temperature probe is arranged in a hearth at the outlet of the kiln body air inlet channel.
Preferably, the system is provided with a plurality of said temperature probes. The number of the plurality of temperature probes is 1 to 50, preferably 2 to 30, and more preferably 3 to 15.
Preferably, the system is further provided with a kiln head support. The kiln head supporting piece is arranged in the annular air inlet channel and connected with two side walls of the annular air inlet channel.
Preferably, the incineration rotary kiln is of an inclined design with a kiln head higher than a kiln tail, and the inclination angle is 3-60 degrees, preferably 5-45 degrees, and more preferably 8-30 degrees.
A hazardous waste pyrolytic incineration temperature control method or a method for performing hazardous waste pyrolytic incineration temperature control using the system of the first embodiment, the method comprising the steps of:
1) and conveying pyrolysis residues of the hazardous wastes subjected to pyrolysis in the pyrolysis rotary kiln into the incineration rotary kiln for incineration treatment according to the trend of the materials. And discharging the incineration residue after incineration from an incineration discharge port.
2) According to the trend of the flue gas, the high-temperature flue gas of the incineration rotary kiln is conveyed to the pyrolysis rotary kiln to provide heat for material pyrolysis. And conveying pyrolysis gas generated by pyrolysis of the pyrolysis rotary kiln into the incineration rotary kiln to provide fuel for material incineration, and circulating the steps.
3) In the burning rotary kiln, the pyrolyzed materials are put into a hearth through a material inlet channel for burning treatment. Meanwhile, pyrolysis gas generated by pyrolysis is conveyed to the annular gas inlet channel and then conveyed to the hearth through the kiln body gas inlet channel for combustion. In the process, the temperature probes monitor the change condition of the incineration temperature in the hearth in real time. Finally, the purpose of adjusting the incineration temperature in the hearth is achieved by adjusting the input amount of materials (or fuel) or adjusting the input amount of pyrolysis gas input by the kiln body gas inlet channel.
Preferably, step 3) is specifically:
301) and monitoring the incineration temperature of each area in the hearth to be Ti and DEG C in real time through a plurality of temperature probes. i is the total number of temperature probes. The average temperature of incineration in the hearth is recorded as Tp and DEG C. Then:
tp ═ T1+ T2+ T3+. + Ti)/I.
ST＝[(T1-Tp)2+(T2-Tp)2+(T3-Tp)2+...(Ti-Tp)2]Formula II.
Formula II, in STIs the variance of the incineration temperature.
302) Setting the ideal burning temperature in the hearth as Ta and DEG C and the ideal temperature fluctuation value as C. And (3) judging:
when Tp is less than (Ta-C), the input amount of pyrolysis gas input by the kiln body air inlet channel is increased by adjusting the air inlet pipeline valve, so that Tp is (Ta +/-C). When Tp (Ta +/-C) cannot be achieved after all pyrolysis gas generated by pyrolysis is input into a hearth, the fuel input amount of the incineration rotary kiln is increased through a heat supplementing fuel pipeline, and the Tp (Ta +/-C) is achieved.
When Tp is greater than (Ta + C), the input amount of pyrolysis gas input from the kiln body gas inlet channel is reduced by adjusting the gas inlet pipeline valve, so that Tp is (Ta +/-C).
When Tp is (Ta ± C), step 303) is performed.
303) Setting the ideal variance of the system as STaAnd then judging:
when S isT≤STaAnd meanwhile, the system maintains the current state to continuously run without any adjustment.
When S isT＞STaThen, the following calculation is performed in sequence:
Tki.e. Ti-Tp i.
In the formula III, TkThe absolute value of the temperature difference between the temperature of each temperature detection point and the average temperature is obtained.
Get TkThe maximum corresponding temperature value Ti. And (4) judging:
303a) when Ti is larger than Tp, the air inlet quantity of the corresponding kiln body inlet channel (203) is reduced until the Ti is equal to (Ta +/-C).
303b) When Ti < Tp, the intake air quantity of the corresponding kiln body intake passage (203) is increased until the Ti is equal to (Ta +/-C).
After completing the adjustment according to 303a) or 303b), return to step 301) and continue monitoring.
Preferably, in step 302), when Tp < (Ta-C), the amount of fuel replenished through the hot fuel pipe is stepped, with each step of replenished fuel being M, kg/h. The value of M is 5-50, preferably 10-40.
Preferably, in step 302), when Tp > (Ta + C), the flow rate of the pyrolysis gas decreased through the kiln inlet passage is divided into steps, and the adjustment amount of the pyrolysis gas decreased in each step is r% based on the total flow rate of the pyrolysis gas.
Preferably, the value of r is 3 to 15, preferably 4 to 12, and more preferably 5 to 10.
Preferably, in step 303), when S isT＞STaWhen the flow of the pyrolysis gas is reduced or increased through the kiln body gas inlet channel, the flow of the pyrolysis gas is reduced or increased step by step, and the adjustment amount of the pyrolysis gas reduced or increased in each step is n percent based on the total flow of the pyrolysis gas.
Preferably, the value of n is 1 to 10, preferably 3 to 8, and more preferably 3 to 5.
In the prior art, the existing rotary incineration kiln device is generally provided with only one air inlet, namely all air required by material incineration enters the rotary kiln from the kiln head, and the air quantity can be adjusted only through the flow of the air in the kiln head. This has two disadvantages: firstly, the air just got into the rotary kiln, can form an oxygen-enriched section at the rotary kiln entrance, and the material is sufficient, violent burning in this section oxygen, and the temperature is higher, and the rotary kiln back end then oxygen is not enough, and the temperature reduces rapidly, has formed the temperature distribution structure that the rotary kiln forward range temperature is high (being too high than ideal temperature value Ta), and the backward range temperature is low (being too low than ideal temperature value Ta). The normal combustion temperature Ta of the materials in the rotary kiln is generally guaranteed to be 850-900 ℃, when the high temperature in the rotary kiln is too high, ash slag is easy to melt, and when the temperature is too low, the molten ash slag is condensed, so that the ring formation phenomenon is caused. Secondly, because the solid material is not uniformly contacted with the air, part of residues can not be fully combusted, and the generation of dioxin can be increased.
Further, among the prior art, the required fuel of section of burning mainly comes from material and pyrolysis gas after the pyrolysis of pyrolysis section, owing to the adoption be kiln head feeding and air inlet simultaneously, and then the burning phenomenon in the rotary kiln antecedent process is violent and thorough, and the burning phenomenon appears in the rotary kiln antecedent process and can consume a large amount of fuel and pyrolysis gas to make the fuel and the pyrolysis gas that flow into the back process and supply to burn the processing not enough, cause follow-up burning treatment combustion temperature lower, generate a large amount of dioxin easily. Meanwhile, the temperature of the incineration rotary kiln along the direction of the kiln body is not uniformly distributed, so that the incineration efficiency is not high, and the ring formation phenomenon is easy to occur at a high-temperature section, thereby influencing the normal production.
The invention provides an organic hazardous waste treatment process for dividing the existing integrated incineration rotary kiln into a pyrolysis kiln and an incineration kiln, wherein the pyrolysis and incineration of materials are respectively realized in the two kilns, namely a pyrolysis section and an incineration section are relatively independent. Wherein high-temperature flue gas generated by burning in the burning rotary kiln is introduced into the pyrolysis rotary kiln through a pipeline to provide heat for material pyrolysis. Combustible pyrolysis gas generated by pyrolysis of the pyrolysis rotary kiln enters the kiln along the kiln body of the incineration rotary kiln through a pipeline in a multi-stage conveying mode to be burnt as fuel, and the fuel in the kiln is uniformly distributed in a multi-stage sectional conveying mode of the pyrolysis gas along the kiln body, so that the uniform incineration temperature in the kiln is ensured.
In the invention, in order to effectively control the temperature distribution in the hearth of the incineration rotary kiln to be uniform, a kiln head of the pyrolysis rotary kiln is respectively provided with a material inlet channel, a combustion-supporting air channel, a pyrolysis gas inlet pipeline and a heat supplementing fuel pipeline which are not communicated with each other, a plurality of kiln body inlet channels are arranged in a furnace lining of a kiln body of the pyrolysis rotary kiln, the lengths of the plurality of kiln body inlet channels are sequentially increased, namely gas outlets of the plurality of kiln body inlet channels are uniformly distributed along the direction from the kiln head to the kiln tail, so that pyrolysis gas conveyed into the hearth is uniformly distributed, and the temperature distribution in the hearth is uniform by heat released during combustion. The air outlet of each of the air inlet channels of the kiln bodies is provided with an air inlet nozzle with a certain height, the air inlet nozzles extend into the hearth from the kiln lining, the opening direction of the nozzles faces away from the direction of the supplied materials, and the outlet planes of the nozzles are provided with separation nets of net-shaped steel structures, so that the materials are prevented from falling into air pipes in the advancing process to cause air pipe blockage. Meanwhile, in order to further improve the incineration effect, the lining of the incineration rotary kiln is made of materials with heat preservation effect, the thickness of the lining is 3-50cm (preferably 5-30cm, and more preferably 8-15cm), the hearth is completely covered by the lining, and heat loss is reduced. The emission of excessive thermal radiation to the outside is also avoided.
In the invention, a plurality of temperature probes (the temperature probes are arranged at the intersection of the air inlet spray heads in the air injection direction, and at least one temperature probe is arranged at the accessory of each air inlet spray head) are arranged in the hearth to monitor the temperature change of each area in the hearth in real time, and the system is adjusted according to the change, so that the temperature of each area in the hearth is uniform and is in the optimal ideal temperature range. The method comprises the following specific steps:
301) and monitoring the incineration temperature of each area in the hearth to be Ti and DEG C in real time through a plurality of temperature probes. i is the total number of temperature probes. The average temperature of incineration in the hearth is recorded as Tp and DEG C. Then:
tp ═ T1+ T2+ T3+. + Ti)/I.
ST＝[(T1-Tp)2+(T2-Tp)2+(T3-Tp)2+...(Ti-Tp)2]Formula II.
Formula II, in STIs the variance of the incineration temperature. Then step 301) and step 302) are performed in this order.
302) Setting the ideal burning temperature in the hearth as Ta and DEG C and the ideal temperature fluctuation value as C. And (3) judging:
when Tp is less than (Ta-C), the input amount of pyrolysis gas input by the kiln body air inlet channel is increased by adjusting the air inlet pipeline valve, so that Tp is (Ta +/-C). When Tp (Ta +/-C) cannot be achieved after all pyrolysis gas generated by pyrolysis is input into a hearth, the fuel input amount of the incineration rotary kiln is increased through a heat supplementing fuel pipeline, and the Tp (Ta +/-C) is achieved.
In the present invention, the fuel may be a pyrolysis material obtained by pyrolyzing hazardous waste, and may also be other solid fuel (such as pulverized coal, carbon powder, etc.), or liquid fuel (such as kerosene, gasoline), or gaseous fuel (such as methane, hydrogen, etc.).
When Tp is greater than (Ta + C), the input amount of pyrolysis gas input from the kiln body gas inlet channel is reduced by adjusting the gas inlet pipeline valve, so that Tp is (Ta +/-C).
When Tp is (Ta ± C), step 303) is performed.
303) Setting the ideal variance of the system as STaAnd judging:
preferably, when S isT≤STaAnd meanwhile, the system maintains the current state to continuously run without any adjustment.
Preferably, when S isT＞STaThen, the following calculation is performed in sequence:
Tki.e. Ti-Tp i.
In the formula III, TkThe absolute value of the temperature difference between the temperature of each temperature detection point and the average temperature is obtained.
Get TkAnd (3) judging the maximum corresponding temperature value Ti:
303a) when Ti is larger than Tp, the air inlet quantity of the corresponding kiln body inlet channel (203) is reduced until the Ti is equal to (Ta +/-C).
303b) When Ti < Tp, the intake air quantity of the corresponding kiln body intake passage (203) is increased until the Ti is equal to (Ta +/-C).
After completing the adjustment according to 303a) or 303b), return to step 301) and continue monitoring.
Further, in step 302), when Tp < (Ta-C), the amount of fuel supplemented through the heat-supplementing fuel pipe is stepped, and the amount of fuel supplemented in each step is M, kg/h. The value of M is 5-50 (preferably 10-40, and more preferably 15-30), it is required to be mentioned that the fuel supplement operation is performed when all the pyrolysis gas is delivered into the hearth and combusted, and the temperature is still not adjusted to be uniform.
In step 302), when Tp > (Ta + C), the flow of the pyrolysis gas reduced through the kiln body air inlet channel is performed in steps, and the adjustment amount of the reduced pyrolysis gas in each step is r% based on the total flow of the pyrolysis gas. The value of r is 3-15, preferably 4-12, more preferably 5-10. Preferred adjustment recommendations are as follows: a negative value for the total gas turndown percentage indicates a reduced pyrolysis gas flow and a positive value indicates an increased pyrolysis gas flow. (not to be considered as limiting the invention's concept herein)
Figure RE-GDA0002625560800000061
In step 303), when ST＞STaWhen the method is used, the flow of the pyrolysis gas reduced or increased through the kiln body gas inlet channel is performed step by step, and the adjustment amount of the reduced pyrolysis gas in each step is n percent based on the total flow of the pyrolysis gas. The value of n is 1-10, preferably 3-8, and more preferably 3-5. Preferred adjustment recommendations are as follows: a negative value for the gas flow adjustment percentage indicates a reduced pyrolysis gas flow and a positive value indicates an increased pyrolysis gas flow. (not to be considered as limiting the invention's concept herein)
Figure RE-GDA0002625560800000062
Figure RE-GDA0002625560800000071
After the adjustment is completed, the control routine is restarted until the temperature profiles of the respective sections meet the requirements of the ideal temperature profile as shown in fig. 9.
It should be noted that the calculation (repeating the calculation judgment and adjustment procedure of formula I-III) is required for each adjustment of the fuel charge or the pyrolysis gas transport amount. Basically, the greater the temperature difference (Tk) or the greater the temperature fluctuation range (S)TGreater than STaThe more the value is), the larger the regulating value of the single fuel or pyrolysis gas is (so as to equalize the temperature of each area in the kiln as soon as possible), but on the premise of not influencing the stable operation of the system, the reasonable adjustment can be carried out according to the actual working conditionAnd (5) designing.
In the invention, when the flow rate of the pyrolysis gas conveyed to the hearth needs to be reduced, because the amount of the pyrolysis gas generated by the pyrolysis rotary kiln is certain, the redundant pyrolysis gas can be conveyed to other equipment (such as a boiler) which needs to combust the pyrolysis gas by arranging the bypass pipeline on the pyrolysis gas inlet pipeline.
In the invention, the organic hazardous waste materials before entering the pyrolysis rotary kiln need to be crushed and sieved, wherein only oversize fine materials (the particle size of which is less than or equal to 15mm, preferably less than or equal to 12mm, and more preferably less than or equal to 10mm) are conveyed to the pyrolysis rotary kiln for pyrolysis, and undersize coarse materials (the particle size of which is greater than or equal to 15mm, preferably greater than or equal to 12mm, and more preferably greater than or equal to 10mm) and pyrolysis residues formed after pyrolysis of the oversize fine materials are conveyed to the incineration rotary kiln for incineration treatment. The small particle material has large specific surface area and high pyrolysis efficiency, and is firstly put into a pyrolysis rotary kiln for pyrolysis. The pyrolysis rotary kiln is an external heating rotary kiln, and a pyrolysis heat source is provided by high-temperature flue gas. The material is pyrolyzed under the condition of isolating air, combustible gas can be separated out, and the residual pyrolysis residue is discharged from the pyrolysis rotary kiln. Because the pyrolysis rotary kiln can not ensure that the organic matters in the materials fully react, the pyrolysis residues still have more organic combustible substances, and therefore, the pyrolysis residues are continuously sent into the incineration rotary kiln to be incinerated in the next step. And the large-particle materials are lower in pyrolysis efficiency in the pyrolysis rotary kiln, so that the large-particle materials are directly mixed with pyrolysis residues and then are sent into the incineration rotary kiln to be incinerated together.
In the invention, the pyrolysis residue is fully combusted and decomposed in the incineration rotary kiln, the final bottom slag is discharged from the kiln body for other treatment, meanwhile, combustible pyrolysis gas generated by the pyrolysis rotary kiln is independently extracted and sent into the incineration rotary kiln, the gas (pyrolysis gas) is introduced along the kiln body in a grading way by adopting the design of a plurality of kiln body gas inlet channels, and then air is supplemented from the head of the incineration rotary kiln, so that the full combustion is ensured. And the temperature of the high-temperature flue gas after heat exchange in the pyrolysis furnace is reduced to become low-temperature flue gas. The low-temperature flue gas enters a subsequent waste heat utilization device (such as a waste heat boiler) to recover heat, and then enters a flue gas purification system to be purified and then is discharged.
In the invention, in order to prevent the air current backflow phenomenon, valves or induced draft fans can be arranged on each gas pipeline according to actual requirements. The air flow backflow can be prevented, and the air flow conveying efficiency can be improved.
Furthermore, the annular air inlet channel and the kiln body air inlet channel can be used for conveying fuel gas such as pyrolysis gas and the like, and can also be used for conveying combustion-supporting air for each region in the hearth. Namely, when the delivered pyrolysis gas is sufficient, the pyrolysis gas inlet pipeline can be closed, and the combustion-supporting air delivery pipeline is opened to supplement the combustion-supporting air. When necessary, the pyrolysis gas inlet pipeline, the combustion air conveying pipeline and the annular gas inlet pipeline can be connected by a three-way valve.
In the invention, the kiln length and the outer diameter of the pyrolysis rotary kiln and the incineration rotary kiln can be designed according to actual working conditions. For example, the pyrolysis rotary kiln or the incineration rotary kiln has a furnace length of 3 to 30m, preferably 5 to 25m, and more preferably 8 to 20 m. The outer diameter of the pyrolysis rotary kiln is 1-10m, preferably 2-8m, and more preferably 3-8 m. This is merely an example of a preferred design of the invention and should not be taken as a basis for limiting the scope of the invention.
Furthermore, the feeding amount of the incineration rotary kiln is 800-6000kg/h, preferably 1200-5000kg/h, and more preferably 1500-4000 kg/h. The rotary speed of the burning rotary kiln is 1-6r/min, preferably 1.5-5r/min, and more preferably 2-4 r/min.
In the present invention, 4 pyrolysis gas outlets (arranged from the kiln head to the kiln tail) are arranged along the circumferential direction of the kiln body, and the kiln body is divided into 4 control sections according to the length direction for illustration. The flow rates of 4 pyrolysis gas outlets are respectively Q1～Q4Each corresponding segment has a temperature T1～T4The ratio of the flow of each air outlet to the total flow is a1～a4After the multi-stage kiln body air inlet device is adopted, in order to make the temperature of each section of the kiln body more uniform, the flow rate of each air inlet (based on the total pyrolysis gas inlet amount) is shown in the table below. (neither should they be taken as an admission of the present inventionBasis for protocol limitations):
air inlet position Marking Ratio of occupation of
Kiln body air inlet 1 a1 0.2～0.25
Kiln body air inlet 2 a2 0.2～0.25
Kiln body air inlet 3 a3 0.25～0.3
Kiln body air inlet 4 a4 0.3～0.4
Compared with the prior art, the invention has the following beneficial technical effects:
1. the pyrolysis section and the incineration section of the system adopt a separated design, the high-temperature flue gas in the incineration section is used as a heat source of the pyrolysis section, and the pyrolysis gas in the pyrolysis section is used for assisting the incineration section to burn to obtain the high-temperature flue gas, so that the comprehensive utilization of resources is realized, and the production input cost is reduced.
2. In the incineration rotary kiln, the mode of multi-stage air inlet and multi-point temperature detection of the kiln body is adopted, so that the temperature distribution of the kiln body is more uniform, the temperature distribution is more flexibly adjusted, the combustion efficiency can be improved, and the generation of pollutants such as NOx, dioxin and the like is reduced.
3. The pyrolysis incineration system is simple in structure and easy to operate, and after the temperature distribution is more uniform, the temperature of the traditional rotary kiln is not too high or too low, so that the kiln caking phenomenon of the rotary kiln is reduced mechanically, and the system failure rate is reduced.
Drawings
FIG. 1 is a block diagram of a hazardous waste pyrolysis incineration system according to the present invention.
Fig. 2 is a diagram of a pyrolysis incineration apparatus of a rotary kiln in the prior art.
FIG. 3 is a cross-sectional view of a prior art rotary kiln A-A.
Fig. 4 is a structural diagram of the rotary incineration kiln of the invention.
FIG. 5 is a D-D sectional view of the rotary kiln for incineration according to the present invention.
FIG. 6 is a cross-sectional view of an incineration rotary kiln E-E according to the invention.
Fig. 7 is a view of the rotary incineration kiln F according to the invention.
Fig. 8 is a flow chart of temperature control of the rotary incineration kiln according to the invention.
FIG. 9 is an idealized temperature profile for each section of the rotary kiln.
Reference numerals: a: pyrolyzing the rotary kiln; b: burning the rotary kiln; l1: a first conduit; l2: a second conduit; l3: a third pipeline; 1: a kiln head; 2. a hearth; 3: incinerating a discharge port; 101: a material inlet channel; 102: a combustion air passage; 103: an annular air intake passage; 104: a pyrolysis gas inlet pipeline; 105: a heat-replenishing fuel conduit; 201: a furnace lining; 202: a hearth; 203: a kiln body air inlet channel; 204: an air inlet nozzle; 205: separating the net; 206: an air intake duct valve; 207: a temperature probe; 208: kiln head support piece.
Detailed Description
The technical solution of the present invention is illustrated below, and the claimed scope of the present invention includes, but is not limited to, the following examples.
The utility model provides a hazardous waste pyrolysis system of burning, this system is rotary kiln system of burning, includes pyrolysis rotary kiln A and burns rotary kiln B. The discharge outlet of the pyrolysis rotary kiln A is connected to the feed inlet of the incineration rotary kiln B through a first pipeline L1. The exhaust port of the pyrolysis rotary kiln a is also connected to the intake passage of the incineration rotary kiln B through a second pipe L2. And the smoke outlet of the incineration rotary kiln B is connected to the smoke inlet of the pyrolysis rotary kiln A through a third pipeline L3. Wherein, the burning rotary kiln B comprises a kiln head 1, a kiln body 2 and a burning discharge port 3. The kiln head 1 is provided with a material inlet channel 101, a combustion air channel 102 and an annular air inlet channel 103. The kiln body 2 comprises a furnace lining 201 and a hearth 202. The material inlet channel 101 and the combustion-supporting air duct 102 both penetrate through the kiln head 1 and then are communicated to the hearth 202. The annular inlet channel 103 is arranged inside the kiln head 1. A kiln body air inlet channel 203 is also arranged in the furnace lining 201. One end of the kiln body air inlet channel 203 is communicated with the annular air inlet channel 103. The other end of the kiln body air inlet channel 203 is communicated with the hearth 202.
Preferably, the system also comprises a pyrolysis gas inlet pipeline 104 and a heat supplementing fuel pipeline 105. The pyrolysis gas inlet pipeline 104 and the heat supplementing fuel pipeline 105 are both arranged on the kiln head 1. Wherein, the pyrolysis gas inlet pipe 104 is communicated with the annular gas inlet channel 103. The heat supplementing fuel pipeline 105 penetrates through the kiln head 1 and is communicated with the hearth 202.
Preferably, the system further includes an inlet showerhead 204. The gas inlet nozzle 204 is arranged in the hearth 202 and is connected with the gas outlet of the annular gas inlet channel 103.
Preferably, the gas injection ports of the gas injection nozzles 204 are directed toward the discharge port 3. Further preferably, a screen 205 is disposed at an air injection port of the air intake nozzle 204.
Preferably, the system also comprises a plurality of kiln body air inlet channels 203. A plurality of kiln body air inlet channels 203 are uniformly distributed in the furnace lining 201.
Preferably, the lengths of the kiln inlet channels 203 in the direction from the kiln head 1 to the kiln body 2 are the same or different. Preferably, the lengths of the kiln inlet channels 203 in the direction from the kiln head 1 to the kiln body 2 are increased in sequence.
Preferably, the number of the plurality of kiln body air inlet channels 203 is 1-20, preferably 2-15, and more preferably 3-10.
Preferably, the system also includes an intake manifold valve 206. The inlet pipeline valve 206 is arranged on the furnace lining 201 corresponding to the kiln body inlet channel 203. The opening degree of the kiln body air inlet channel 203 is controlled by adjusting the air inlet pipeline valve 206. The number of the inlet pipeline valves 206 is the same as that of the kiln body inlet channels 203.
Preferably, the system further comprises a temperature probe 207. The temperature probe 207 is disposed within the furnace 202.
Preferably, the temperature probe 207 is arranged in the hearth 202 at the outlet of the kiln body inlet channel 203.
Preferably, the system is provided with a plurality of said temperature probes 207. The number of the plurality of temperature probes 207 is 1 to 50, preferably 2 to 30, and more preferably 3 to 15.
Preferably, the system is further provided with a kiln head support 208. The kiln head support 208 is disposed within the annular inlet passage 103 and is connected to both side walls of the annular inlet passage 103.
Preferably, the incineration rotary kiln B is an inclined design with a kiln head 1 higher than a kiln tail, and the inclination angle is 3-60 degrees, preferably 5-45 degrees, and more preferably 8-30 degrees.
A hazardous waste pyrolytic incineration temperature control method or a method for performing hazardous waste pyrolytic incineration temperature control using the system of the first embodiment, the method comprising the steps of:
1) and (3) according to the trend of the materials, conveying pyrolysis residues of the hazardous wastes subjected to pyrolysis in the pyrolysis rotary kiln A to an incineration rotary kiln B for incineration treatment. The incineration residue after the incineration is discharged from the incineration discharge port 3.
2) According to the trend of the flue gas, the high-temperature flue gas of the incineration rotary kiln B is conveyed into the pyrolysis rotary kiln A to provide heat for material pyrolysis. And (4) conveying pyrolysis gas generated by pyrolysis of the pyrolysis rotary kiln A into the incineration rotary kiln B to provide fuel for material incineration, and circulating the steps.
3) In the rotary incineration kiln B, the pyrolyzed material is fed into the hearth 202 through the material inlet passage 101 for incineration treatment. Meanwhile, pyrolysis gas generated by pyrolysis is conveyed to the annular gas inlet channel 103 and then conveyed to the hearth 202 through the kiln body gas inlet channel 203 for combustion. In the process, a plurality of temperature probes 207 monitor the change of the incineration temperature in the hearth 202 in real time. Finally, the purpose of adjusting the incineration temperature in the hearth 202 is achieved by adjusting the input amount of materials or fuel or adjusting the input amount of pyrolysis gas input by the kiln body gas inlet channel 203.
Preferably, step 3) is specifically:
301) and monitoring the incineration temperature of each area in the hearth to be Ti and DEG C in real time through a plurality of temperature probes 207. i is the total number of temperature probes 207. The average temperature of the combustion in the furnace 202 is denoted as Tp, DEG C. Then:
tp ═ T1+ T2+ T3+. + Ti)/I.
ST＝[(T1-Tp)2+(T2-Tp)2+(T3-Tp)2+...(Ti-Tp)2]Formula II.
Formula II, in STIs the variance of the incineration temperature.
302) The ideal incineration temperature in the furnace 202 is set to Ta and DEG C, and the ideal temperature fluctuation value is set to C. And (3) judging:
when Tp < (Ta-C), the input amount of pyrolysis gas input into the kiln body air inlet channel 203 is increased by adjusting the air inlet pipeline valve 206, so that Tp is (Ta +/-C). When Tp is not equal to (Ta ± C) even after all the pyrolysis gas generated by pyrolysis is input to the furnace 202, the fuel input amount of the incineration rotary kiln B is increased by the heat supply fuel pipe 105, so that Tp is equal to (Ta ± C).
When Tp > (Ta + C), the input amount of pyrolysis gas input into the kiln body air inlet channel 203 is reduced by adjusting the air inlet pipeline valve 206, so that Tp is (Ta +/-C).
When Tp is (Ta ± C), step 303) is performed.
303) Setting the ideal variance of the system as STaAnd judging:
when S isT≤STaAnd meanwhile, the system maintains the current state to continuously run without any adjustment.
When S isT＞STaThen, the following calculation is performed in sequence:
Tki.e. Ti-Tp i.
In the formula III, TkThe absolute value of the temperature difference between the temperature of each temperature detection point and the average temperature is obtained.
Get TkAnd (3) judging the maximum corresponding temperature value Ti:
303a) when Ti is larger than Tp, the air inlet quantity of the corresponding kiln body inlet channel (203) is reduced until the Ti is equal to (Ta +/-C).
303b) When Ti < Tp, the intake air quantity of the corresponding kiln body intake passage (203) is increased until the Ti is equal to (Ta +/-C).
After completing the adjustment according to 303a) or 303b), return to step 301) and continue monitoring.
Preferably, in step 302), when Tp < (Ta-C), the amount of fuel replenished through the hot fuel pipe 105 is stepped, with each step of replenishing being M, kg/h. The value of M is 5-50, preferably 10-40.
Preferably, in step 302), when Tp > (Ta + C), the flow rate of the pyrolysis gas decreased through the kiln inlet 203 is divided into steps, and the adjustment amount of the pyrolysis gas decreased in each step is r% based on the total flow rate of the pyrolysis gas.
Preferably, the value of r is 3 to 15, preferably 4 to 12, and more preferably 5 to 10.
Preferably, in step 303), when S isT＞STaIn the process, the flow of the pyrolysis gas reduced or increased through the kiln body gas inlet channel 203 is carried out step by step, and the adjustment amount of the reduced pyrolysis gas in each step is n percent based on the total flow of the pyrolysis gas.
Preferably, the value of n is 1 to 10, preferably 3 to 8, and more preferably 3 to 5.
Example 1
As shown in fig. 1 and 3, a hazardous waste pyrolysis incineration system is a rotary kiln incineration system, and comprises a pyrolysis rotary kiln a and an incineration rotary kiln B. The discharge outlet of the pyrolysis rotary kiln A is connected to the feed inlet of the incineration rotary kiln B through a first pipeline L1. The exhaust port of the pyrolysis rotary kiln a is also connected to the intake passage of the incineration rotary kiln B through a second pipe L2. And the smoke outlet of the incineration rotary kiln B is connected to the smoke inlet of the pyrolysis rotary kiln A through a third pipeline L3. Wherein, the burning rotary kiln B comprises a kiln head 1, a kiln body 2 and a burning discharge port 3. The kiln head 1 is provided with a material inlet channel 101, a combustion air channel 102 and an annular air inlet channel 103. The kiln body 2 comprises a furnace lining 201 and a hearth 202. The material inlet channel 101 and the combustion-supporting air duct 102 both penetrate through the kiln head 1 and then are communicated to the hearth 202. The annular inlet channel 103 is arranged inside the kiln head 1. A kiln body air inlet channel 203 is also arranged in the furnace lining 201. One end of the kiln body air inlet channel 203 is communicated with the annular air inlet channel 103. The other end of the kiln body air inlet channel 203 is communicated with the hearth 202.
Example 2
Example 1 is repeated except that the system further comprises a pyrolysis gas inlet pipe 104 and a supplementary heating fuel pipe 105. The pyrolysis gas inlet pipeline 104 and the heat supplementing fuel pipeline 105 are both arranged on the kiln head 1. Wherein, the pyrolysis gas inlet pipe 104 is communicated with the annular gas inlet channel 103. The heat supplementing fuel pipeline 105 penetrates through the kiln head 1 and is communicated with the hearth 202.
Example 3
Example 2 is repeated except that the system also includes an inlet showerhead 204. The gas inlet nozzle 204 is arranged in the hearth 202 and is connected with the gas outlet of the annular gas inlet channel 103.
Example 4
Example 3 was repeated except that the gas injection ports of the gas injection nozzles 204 were directed toward the discharge port 3. Further preferably, a screen 205 is disposed at an air injection port of the air intake nozzle 204.
Example 5
Embodiment 4 is repeated except that the system further comprises a plurality of kiln body air inlet channels 203. A plurality of kiln body air inlet channels 203 are uniformly distributed in the furnace lining 201.
Example 6
Example 5 was repeated except that the lengths of the plurality of kiln body intake passages 203 in the direction in which the kiln head 1 extends to the kiln body 2 were sequentially increased.
Example 7
Example 6 was repeated except that the number of the plurality of kiln body intake passages 203 was 4.
Example 8
Example 7 is repeated except that the system also includes an inlet manifold valve 206. The inlet pipeline valve 206 is arranged on the furnace lining 201 corresponding to the kiln body inlet channel 203. The opening degree of the kiln body air inlet channel 203 is controlled by adjusting the air inlet pipeline valve 206. The number of the inlet pipeline valves 206 is the same as that of the kiln body inlet channels 203.
Example 9
Example 8 is repeated except that the system also includes a temperature probe 207. The temperature probe 207 is disposed within the furnace 202.
Example 10
Example 9 was repeated except that the temperature probe 207 was disposed in the furnace 202 at the outlet of the kiln inlet channel 203.
Example 11
Example 10 was repeated except that the system was provided with a plurality of the temperature probes 207. The number of the plurality of temperature probes 207 is 8.
Example 12
Example 11 is repeated, except that the system is also provided with a kiln head support 208. The kiln head support 208 is disposed within the annular inlet passage 103 and is connected to both side walls of the annular inlet passage 103.
Example 13
Example 12 was repeated except that the incineration rotary kiln B was an inclined design with the kiln head 1 higher than the kiln tail, and the inclination angle was 9 °.

Claims (10)

1. A hazardous waste pyrolysis incineration system, characterized in that: the system is a rotary kiln incineration system and comprises a pyrolysis rotary kiln (A) and an incineration rotary kiln (B); the discharge port of the pyrolysis rotary kiln (A) is connected to the feed port of the incineration rotary kiln (B) through a first pipeline (L1); the exhaust port of the pyrolysis rotary kiln (A) is also connected to the air inlet channel of the incineration rotary kiln (B) through a second pipeline (L2); the smoke outlet of the incineration rotary kiln (B) is connected to the smoke inlet of the pyrolysis rotary kiln (A) through a third pipeline (L3); wherein, the burning rotary kiln (B) comprises a kiln head (1), a kiln body (2) and a burning discharge port (3); the kiln head (1) is provided with a material inlet channel (101), a combustion air channel (102) and an annular air inlet channel (103); the kiln body (2) comprises a furnace lining (201) and a hearth (202); the material inlet channel (101) and the combustion-supporting air duct (102) penetrate through the kiln head (1) and are communicated to the hearth (202); the annular air inlet channel (103) is arranged inside the kiln head (1); a kiln body air inlet channel (203) is also arranged in the furnace lining (201); one end of the kiln body air inlet channel (203) is communicated with the annular air inlet channel (103); the other end of the kiln body air inlet channel (203) is communicated with the hearth (202).
2. The system of claim 1, wherein: the system also comprises a pyrolysis gas inlet pipeline (104) and a heat supplementing fuel pipeline (105); wherein the pyrolysis gas inlet pipeline (104) is communicated with the annular gas inlet channel (103); the heat supplementing fuel pipeline (105) penetrates through the kiln head (1) and is communicated with the hearth (202).
3. The system according to claim 1 or 2, characterized in that: the system also includes an inlet showerhead (204); the air inlet spray head (204) is arranged in the hearth (202) and is connected with an air outlet of the annular air inlet channel (103);
preferably, the gas injection openings of the gas inlet nozzle (204) face the direction of the discharge opening (3); further preferably, a separation net (205) is arranged at an air injection port of the air inlet nozzle (204).
4. The system according to any one of claims 1-3, wherein: the system also comprises a plurality of kiln body air inlet channels (203); the plurality of kiln body air inlet channels (203) are uniformly distributed in the furnace lining (201);
preferably, the lengths of the kiln body air inlet channels (203) in the direction from the kiln head (1) to the kiln body (2) are the same or different; preferably, the lengths of the plurality of kiln body air inlet channels (203) in the direction from the kiln head (1) to the kiln body (2) are sequentially increased;
preferably, the number of the kiln body air inlet channels (203) is 1-20, preferably 2-15, and more preferably 3-10.
5. The system according to any one of claims 1-4, wherein: the system also includes an intake manifold valve (206); the air inlet pipeline valve (206) is arranged on a furnace lining (201) corresponding to the kiln body air inlet channel (203); the opening and closing degree of a kiln body air inlet channel (203) is controlled by adjusting an air inlet pipeline valve (206); the number of the air inlet pipeline valves (206) is consistent with that of the kiln body air inlet channels (203).
6. The system according to any one of claims 1-5, wherein: the system also includes a temperature probe (207); the temperature probe (207) is arranged in the hearth (202); preferably, the temperature probe (207) is arranged in a hearth (202) at the outlet of the kiln body air inlet channel (203);
preferably, the system is provided with a plurality of said temperature probes (207); the number of the plurality of temperature probes (207) is 1 to 50, preferably 2 to 30, and more preferably 3 to 15.
7. The system of claim 6, wherein: the system is also provided with a kiln head support (208); the kiln head supporting piece (208) is arranged in the annular air inlet channel (103) and connected with two side walls of the annular air inlet channel (103); and/or
The incineration rotary kiln (B) is designed in an inclined mode that the kiln head (1) is higher than the kiln tail, and the inclination angle is 3-60 degrees, preferably 5-45 degrees, and more preferably 8-30 degrees.
8. A hazardous waste pyrolysis incineration temperature control method or a method for performing hazardous waste pyrolysis incineration temperature control using the system according to any one of claims 1 to 7, characterized in that: the method comprises the following steps:
1) according to the trend of materials, the pyrolysis residues of the hazardous wastes after pyrolysis in the pyrolysis rotary kiln (A) are conveyed to an incineration rotary kiln (B) for incineration treatment; the incineration residue after the incineration is finished is discharged from an incineration discharge port (3);
2) according to the trend of the flue gas, conveying the high-temperature flue gas of the incineration rotary kiln (B) to the pyrolysis rotary kiln (A) to provide heat for material pyrolysis; pyrolysis gas generated by pyrolysis of the pyrolysis rotary kiln (A) is conveyed into the incineration rotary kiln (B) to provide fuel for material incineration, and circulation is carried out according to the fuel;
3) in the burning rotary kiln (B), the pyrolyzed materials are put into a hearth (202) through a material inlet channel (101) for burning treatment; meanwhile, pyrolysis gas generated by pyrolysis is conveyed to the annular gas inlet channel (103) and then conveyed to the hearth (202) through the kiln body gas inlet channel (203) to be combusted; in the process, a plurality of temperature probes (207) monitor the change condition of the incineration temperature in the hearth (202) in real time; finally, the purpose of adjusting the incineration temperature in the hearth (202) is achieved by adjusting the input amount of materials (or fuel) or adjusting the input amount of pyrolysis gas input by the kiln body gas inlet channel (203).
9. The method of claim 8, wherein: the step 3) is specifically as follows:
301) monitoring the incineration temperature of each area in the hearth (202) to be Ti and DEG C in real time through a plurality of temperature probes (207); i is the total number of the temperature probes (207); the average temperature of burning in the hearth (202) is recorded as Tp and DEG C; then:
tp ═ T1+ T2+ T3+. + Ti)/I.. formula I;
ST＝[(T1-Tp)2+(T2-Tp)2+(T3-Tp)2+...(Ti-Tp)2]formula II;
formula II, in STIs the variance of the incineration temperature;
302) setting an ideal incineration temperature in a hearth (202) as Ta and DEG C and an ideal temperature fluctuation value as C; and (3) judging:
when Tp < (Ta-C), increasing the input amount of pyrolysis gas input by a kiln body gas inlet channel (203) by adjusting a gas inlet pipeline valve (206) so that Tp is (Ta +/-C); when Tp (Ta +/-C) cannot be achieved after all pyrolysis gas generated by pyrolysis is input into a hearth (202), the fuel input amount of the incineration rotary kiln (B) is increased through a heat supplementing fuel pipeline (105), and the Tp (Ta +/-C) is achieved;
when Tp is > (Ta + C), reducing the input amount of pyrolysis gas input by a kiln body gas inlet channel (203) by adjusting a gas inlet pipeline valve (206) so that Tp is (Ta +/-C);
when Tp is (Ta ± C), step 303) is performed;
303) setting the ideal variance of the system as STaAnd judging:
when S isT≤STaMeanwhile, the system maintains the current state to continue running without any adjustment;
when S isT＞STaThen, the following calculation is performed in sequence:
Tki.e. Ti-Tp i.e. formula III;
in the formula III, TkTaking the absolute value of the difference between the temperature of each temperature detection point and the average temperaturekAnd (3) judging the maximum corresponding temperature value Ti:
303a) when Ti is more than Tp, reducing the air intake quantity of the corresponding kiln body air intake channel (203) until the Ti at the position is equal to (Ta +/-C);
303b) when Ti is less than Tp, increasing the air intake quantity of the corresponding kiln body air intake channel (203) until the Ti is equal to (Ta +/-C);
after completing the adjustment according to 303a) or 303b), return to step 301) and continue monitoring.
10. The method of claim 9, wherein: in step 302), the fuel quantity supplemented through the heat supplementing fuel pipeline (105) is carried out step by step, and the supplemented fuel quantity in each step is M, kg/h; the value of M is 5-50, preferably 10-40; and/or
In step 302), when Tp > (Ta + C), the flow of the pyrolysis gas reduced by the kiln body gas inlet channel (203) is carried out in steps, and the adjustment amount of the reduced pyrolysis gas in each step is r percent based on the total flow of the pyrolysis gas; the value of r is 3-15, preferably 4-12, more preferably 5-10; and/or
In step 303), when ST＞STaWhen the flow of the pyrolysis gas is reduced or increased through the kiln body gas inlet channel (203), the flow of the pyrolysis gas is stepped, and the adjustment amount of the reduced or increased pyrolysis gas in each step is n percent based on the total flow of the pyrolysis gas; the value of n is 1-10, preferably 3-8, and more preferably 3-5.
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