CN113028409B - Method for clean combustion of gas by synergistic treatment of straw domestic garbage - Google Patents

Method for clean combustion of gas by synergistic treatment of straw domestic garbage Download PDF

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Publication number
CN113028409B
CN113028409B CN202110596569.9A CN202110596569A CN113028409B CN 113028409 B CN113028409 B CN 113028409B CN 202110596569 A CN202110596569 A CN 202110596569A CN 113028409 B CN113028409 B CN 113028409B
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combustion
gas
pyrolysis
flue gas
temperature
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CN113028409A (en
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姚宗路
赵立欣
邓云
霍丽丽
贾吉秀
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Institute of Environment and Sustainable Development in Agriculturem of CAAS
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Institute of Environment and Sustainable Development in Agriculturem of CAAS
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    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/04Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment drying
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/14Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44Details; Accessories
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44Details; Accessories
    • F23G5/46Recuperation of heat
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23GCREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00Waste heat recuperation
    • F23G2206/10Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying

Abstract

The invention relates to the technical field of waste treatment, in particular to a clean combustion method for cooperatively treating gas by using straw and domestic garbage. The invention provides a clean combustion method for cooperatively treating gas by using straw and household garbage, which comprises the following steps of: carrying out anoxic combustion on the straws to obtain volatile gas; carrying out oxygen-insulating pyrolysis on the household garbage to obtain pyrolysis gas, wherein the temperature of the oxygen-insulating pyrolysis is 900-1000 ℃; mixing the pyrolysis gas with the volatile gas after heat preservation to obtain initial flue gas, and performing primary combustion and secondary combustion on the initial flue gas to obtain secondary flue gas; the temperature of the pyrolysis gas after heat preservation is 900-1000 ℃; the temperature of the primary combustion is 950-1100 ℃, and the temperature of the secondary combustion is 850-1000 ℃. The combustion efficiency of the pyrolysis gas provided by the method is as high as 97.3%, and the discharged secondary flue gas does not contain dioxin.

Description

Method for clean combustion of gas by synergistic treatment of straw domestic garbage
Technical Field
The invention relates to the technical field of waste treatment, in particular to a clean combustion method for cooperatively treating gas by using straw and domestic garbage.
Background
Compared with the city, because the treatment capacity and the infrastructure are relatively lagged, the rural domestic garbage is difficult to obtain complete, timely and effective treatment, the pollution is brought to the atmosphere, soil and water, and a series of other rural environmental sanitation problems are generated.
As another large waste straw in rural areas, the condition of straw burning in the field still happens occasionally, which causes pollution to the atmosphere.
The domestic garbage pyrolysis technology can effectively realize the recycling, reduction and harmlessness of the domestic garbage, the straw bundle combustion can be used as fuel to replace a coal-fired boiler for combustion heat supply, the combination of the two methods can effectively realize the recycling and harmlessness utilization of rural straws and garbage wastes, and meanwhile, the heating cost in rural areas is reduced.
However, in the actual operation process of the synergistic treatment, when the pyrolysis gas obtained from the household garbage is not subjected to heat preservation or the combustion temperature of the pyrolysis gas is too low, the problems that the combustion efficiency of the mixed gas is low, dioxin is easily generated and the like are easily caused.
Disclosure of Invention
In view of the above, the invention provides a clean combustion method for cooperatively processing fuel gas by using straw and domestic garbage, and the method provided by the invention has higher combustion efficiency of pyrolysis gas, can effectively avoid generation of dioxin by secondary flue gas, and realizes high-efficiency clean combustion of cooperatively processed fuel gas.
In order to achieve the purpose, the invention provides the following technical scheme:
the invention provides a clean combustion method for cooperatively treating gas by using straw and household garbage, which comprises the following steps of:
carrying out anoxic combustion on the straws to obtain volatile gas;
carrying out oxygen-insulating pyrolysis on the household garbage to obtain pyrolysis gas, wherein the temperature of the oxygen-insulating pyrolysis is 900-1000 ℃;
mixing the pyrolysis gas with the volatile gas after heat preservation to obtain initial flue gas, and performing primary combustion and secondary combustion on the initial flue gas to obtain secondary flue gas;
the temperature after heat preservation is 900-1000 ℃;
the temperature of the primary combustion is 950-1100 ℃, and the temperature of the secondary combustion is 850-1000 ℃.
Preferably, the excess air coefficient during the anoxic combustion is 0.8-0.85, and the temperature of the anoxic combustion is 650-750 ℃.
Preferably, the oxygen content during the primary combustion is 8-13%, and the time of the primary combustion is 2-3 s.
Preferably, the excess air coefficient during the primary combustion is 1.2-1.3.
Preferably, the oxygen content during secondary combustion is 10-14%, and the secondary combustion time is 1-2 s.
Preferably, the excess air coefficient during the secondary combustion is 1-1.2.
Preferably, the volatile gas comprises H2、CO、CO2And CxHy
Preferably, before the oxygen-isolated pyrolysis, the domestic garbage is dried at the temperature of 150-200 ℃ for 2-3 hours.
Preferably, after the secondary flue gas is obtained, the secondary flue gas is used for heating the domestic garbage during oxygen insulation pyrolysis to obtain the heat exchange flue gas.
Preferably, after the heat exchange flue gas is obtained, the heat exchange flue gas is used for heating the household garbage during drying.
The invention provides a clean combustion method for cooperatively treating gas by using straw and household garbage, which comprises the following steps of: carrying out anoxic combustion on the straws to obtain volatile gas; carrying out oxygen-insulating pyrolysis on the household garbage to obtain pyrolysis gas, wherein the temperature of the oxygen-insulating pyrolysis is 900-1000 ℃; mixing the pyrolysis gas with the volatile gas after heat preservation to obtain initial flue gas, and performing primary combustion and secondary combustion on the initial flue gas to obtain secondary flue gas; the temperature of the pyrolysis gas after heat preservation is 900-1000 ℃; the temperature of the primary combustion is 950-1100 ℃, and the temperature of the secondary combustion is 850-1000 ℃. According to the invention, the temperature of oxygen-insulating pyrolysis is set to be 900-1000 ℃, the obtained pyrolysis gas is subjected to heat preservation, the temperature after heat preservation is set to be 900-1000 ℃, the pyrolysis gas and volatile gas are mixed and then subjected to primary combustion and secondary combustion, wherein the temperature of the primary combustion is set to be 950-1100 ℃, and the temperature of the secondary combustion is set to be 850-1000 ℃, so that the gas for the synergistic treatment of the straw household garbage is fully and effectively combusted, the combustion efficiency of the pyrolysis gas is high, harmful gases such as dioxin are not generated, and the efficient and clean combustion treatment of the straw and the household garbage is realized. The results of the embodiment show that the combustion efficiency of the pyrolysis gas provided by the method is as high as 97.3%, and the discharged secondary flue gas does not contain dioxin.
Drawings
FIG. 1 is a process route diagram of a method for clean combustion of gas by co-processing straw household garbage according to an embodiment of the present invention;
FIG. 2 is a control route diagram of a method for clean combustion of gas by co-processing straw household garbage according to an embodiment of the present invention;
FIG. 3 is a chromatogram of volatile organic compounds measured after sampling of discharged flue gas when the method for clean combustion of straw household garbage co-processing fuel gas provided by the embodiment of the invention is stable in combustion;
fig. 4 shows the content of the top ten substances in the mass concentration of the volatile organic compounds in the exhaust flue gas when the method for clean combustion of the straw household garbage co-processing fuel gas provided by the embodiment of the invention is stable in combustion.
Detailed Description
The invention provides a clean combustion method for cooperatively treating gas by using straw and household garbage, which comprises the following steps of:
carrying out anoxic combustion on the straws to obtain volatile gas;
carrying out oxygen-insulating pyrolysis on the household garbage to obtain pyrolysis gas, wherein the temperature of the oxygen-insulating pyrolysis is 900-1000 ℃;
mixing the pyrolysis gas with the volatile gas after heat preservation to obtain initial flue gas, and performing primary combustion and secondary combustion on the initial flue gas to obtain secondary flue gas;
the temperature of the pyrolysis gas after heat preservation is 900-1000 ℃;
the temperature of the primary combustion is 950-1100 ℃, and the temperature of the secondary combustion is 850-1000 ℃.
The straw is subjected to anoxic combustion to obtain volatile gas; the invention has no special requirements on the source of the straws, the invention preferably performs pretreatment on the straws, the pretreatment preferably comprises crushing and bundling, the invention has no special requirements on the specific implementation mode of the crushing and bundling, and the straws are preferably used in the mode of straw bundles.
In the invention, the feeding amount of the straw (single bundle of straw) is preferably 300-470 kg/h, and more preferably 380-450 kg/h.
In the invention, the anoxic combustion is preferably carried out in a combustion chamber, the excess air coefficient during the anoxic combustion is preferably 0.8-0.85, more preferably 0.8, and the excess air coefficient during the anoxic combustion is preferably controlled by a fan; in the invention, the temperature of the anoxic combustion is preferably 650-750 ℃, more preferably 680-720 ℃, and most preferably 700-710 ℃; in the invention, the time of the anoxic combustion (single bundle of straws) is preferably 10-15 min, and more preferably 11.5-13 min.
In the present invention, the anoxic combustion is preferably performed by means of co-current combustion, and the present invention has no particular requirement on the specific embodiment of the co-current combustion.
In the present invention, the volatile gas preferably includes H2、CO、CO2And CxHySaid C isxHyPreferably CH4. In the present invention, H in the volatile component2The mass percentage of (A) is preferably 20-23%, the mass percentage of CO is preferably 21-24%, and the mass percentage of CO is preferably 21-24%2The mass percentage of C is preferably 28-32 percent, and C isxHyThe mass percentage of (B) is preferably 20-22%.
According to the invention, the domestic garbage is subjected to oxygen-insulating pyrolysis to obtain pyrolysis gas, wherein the temperature of the oxygen-insulating pyrolysis is 900-1000 ℃; the invention has no special requirements on the source of the household garbage; before the oxygen-isolated pyrolysis, the invention preferably also comprises drying the domestic garbage; in the present invention, it is preferable that the domestic waste is pretreated before being dried, and in the present invention, the pretreatment preferably includes: sorting and dehydrating are sequentially carried out, the recyclable garbage is recycled through sorting, special requirements on the specific implementation of the dehydrating are not required, and after the pretreatment is finished, the water content of the household garbage is preferably less than 30%, more preferably less than 25%; the invention can improve the pyrolysis efficiency of the household garbage through dehydration treatment.
In the invention, the drying temperature is preferably 150-200 ℃, and more preferably 180-190 ℃; the drying time is preferably 2-3 hours, and more preferably 2.5-2.6 hours. In the present invention, the drying is preferably performed in a hopper.
The invention preferably utilizes the dry flue gas generated during drying, and the invention preferably mixes the dry flue gas with the volatile component gas and the pyrolysis gas.
According to the invention, the pyrolysis efficiency of the household garbage can be improved through drying treatment.
In the invention, the feeding amount of the household garbage is preferably 950-1100 kg/h, and more preferably 1033 kg/h.
In the invention, the temperature of the oxygen-insulating pyrolysis is preferably 900-1000 ℃, more preferably 950-980 ℃, in the invention, the oxygen-insulating pyrolysis is preferably carried out in a pyrolysis furnace, and the temperature rise rate of the oxygen-insulating pyrolysis is preferably 150-200 ℃/min, more preferably 165-180 ℃/min; the time for the oxygen-isolated pyrolysis is preferably 35-60 min, more preferably 40-55 min, and most preferably 50 min.
After obtaining volatile gas and pyrolysis gas, the invention mixes the pyrolysis gas with the volatile gas after heat preservation to obtain initial flue gas.
In the invention, the temperature of the pyrolysis gas after heat preservation is preferably 900-1000 ℃, and more preferably 950-980 ℃; in the invention, the pyrolysis gas is conveyed through a pyrolysis gas pipeline, the pyrolysis gas pipeline is preferably positioned in the pyrolysis furnace, and the pyrolysis gas pipeline is preferably tightly attached to the furnace wall in the pyrolysis furnace.
According to the invention, by controlling the temperature of oxygen-insulating pyrolysis and the temperature of pyrolysis gas heat preservation, the temperature of pyrolysis gas can be effectively prevented from being reduced by cooling, and liquid tar formed by condensation blocks a pyrolysis gas pipeline; meanwhile, dioxin generated by low-temperature heterogeneous catalysis of the precursor in the oxygen-insulating pyrolysis process can be avoided.
In the present invention, the mixing is preferably performed in a primary combustion chamber. In the present invention, the mixing is preferably performed after the mixture is ejected through a mixer nozzle, and in the present invention, the mixer nozzle is preferably arranged in a circle, and the mixture gas nozzle is preferably injected at a tangential angle of 5 to 10 °.
After primary flue gas is obtained, the primary flue gas is subjected to primary combustion and secondary combustion to obtain secondary flue gas; the temperature of the primary combustion is 950-1100 ℃, and the temperature of the secondary combustion is 850-1000 ℃.
In the invention, the temperature of the primary combustion is preferably 950-1100 ℃, and more preferably 980-1000 ℃; in the invention, the oxygen content in the primary combustion is preferably 8-13%, more preferably 9-11.5%, and most preferably 10-11%; in the invention, the time of the primary combustion is preferably 2-3 s; in the invention, the excess air coefficient during the primary combustion is preferably 1.2-1.3.
In the present invention, the primary combustion is preferably performed in the primary combustion chamber, and a first air distribution nozzle for injecting first air is preferably provided in the primary combustion chamber; in the present invention, the first air distribution nozzles are preferably arranged in a circle, the first air distribution nozzles preferably inject air at a tangential angle opposite to that of the air mixture nozzle, and the injection angle of the air distribution nozzles is preferably the same as that of the mixer nozzle.
The initial smoke and the first air are subjected to swirl combustion by adjusting the injection direction and the intake angle of the mixed gas nozzle and the first air distribution nozzle in the primary combustion chamber. The primary flue gas obtained by the primary combustion is conveyed to a secondary combustion chamber through a flue gas channel for secondary combustion; in the invention, the smoke channel is preferably provided with the flow baffle plates, the number of the flow baffle plates is preferably 2-3, and the flow baffle plates are preferably arranged in the smoke channel, so that the primary smoke can be baffled for 2-3 times, the retention time of the primary smoke in the primary combustion chamber is prolonged, and the combustion is more sufficient.
In the invention, the preferable temperature of the primary flue gas is 950-1100 ℃.
In the invention, the temperature of the secondary combustion is preferably 850-1000 ℃, and more preferably 900-950 ℃; the oxygen content during secondary combustion is preferably 10-14%, and more preferably 11-13%; the secondary combustion time is preferably 1-2 s; in the invention, the excess air coefficient during the secondary combustion is preferably 1-1.2.
In the present invention, the secondary combustion is preferably performed in the secondary combustion chamber, and in the present invention, the secondary combustion chamber is preferably provided with a second air distribution nozzle for injecting second air; in the invention, the second air distribution nozzle is preferably arranged at an inlet of the secondary combustion chamber connected with the flue gas channel, and the second air distribution nozzle preferably has a flow direction opposite to that of the primary flue gas entering the secondary combustion chamber when spraying the second air, so that the primary flue gas is subjected to disturbance combustion in the secondary combustion chamber.
The temperature of the primary combustion and the secondary combustion is controlled, so that the temperature of the flue gas is prevented from being reduced in the flowing process to generate dioxin.
In the invention, the preferable range of the secondary flue gas is 850-1000 ℃.
The invention preferably carries out heat utilization on the obtained secondary flue gas.
After the secondary flue gas is obtained, the invention preferably further comprises the step of heating the secondary flue gas when the secondary flue gas is used for carrying out oxygen-insulated pyrolysis on the household garbage to obtain heat exchange flue gas; after the heat exchange flue gas is obtained, the invention preferably also comprises the step of heating the heat exchange flue gas when the domestic garbage is dried; the heat exchange flue gas is preferably used for heating the domestic garbage during drying to obtain the final mixed heat flue gas; in the present invention, the final mixed hot flue gas is preferably subjected to heat exchange with water to supply hot water to the outside.
The invention preferably empties the secondary flue gas after heat utilization.
In the present invention, the secondary flue gas preferably includes ethylene, acetylene, ethane, propylene, acetaldehyde, methyl chloride, benzene, acetone, propanal, and propane, and does not contain dioxin.
In order to realize high-efficiency clean combustion of the straw domestic garbage co-processing fuel gas, the straw domestic garbage co-processing fuel gas is fed back by taking the temperature of primary combustion, the oxygen content of the primary combustion, the temperature of secondary combustion and the oxygen content of the secondary combustion as signals, the feeding amount of the straw, the feeding amount of the domestic garbage, the excess air coefficient of the anoxic combustion of the straw and the excess air coefficient of the primary combustion, and a specific feedback route chart is shown in fig. 2.
In the present invention, the feedback (as shown in fig. 2) is preferably: when the temperature of the primary combustion is lower than 950-1100 ℃, increasing the feeding amount of the straws within the range of 380-450 kg/h until the temperature of the primary combustion reaches 950-1100 ℃; and when the oxygen content of the primary combustion is kept to be 8-13%, the excess air coefficient of the anoxic combustion of the straws is increased within the range of 0.8-0.85, the excess air coefficient of the primary combustion is increased within the range of 1.2-1.3, and meanwhile, the feeding amount of the household garbage is reduced within the range of 950-1033 kg/h.
When the temperature of the primary combustion is higher than 950-1100 ℃, reducing the feeding amount of the straws to the temperature of the primary combustion within the range of 300-380 kg/h; and simultaneously, the excess air coefficient of the primary combustion is reduced within the range of 1.2-1.3 so as to reach 950-1100 ℃.
When the temperature of the secondary combustion is lower than 850-1000 ℃, the temperature of the primary combustion is increased within the range of 950-1100 ℃; when the oxygen content of the secondary combustion is kept to be 10-14%, the excess air coefficient during the secondary combustion is reduced within the range of 1-1.2, and meanwhile, the feeding amount of the household garbage is reduced within the range of 950-1033 kg/h.
And when the temperature of the secondary combustion is higher than 850-1000 ℃, reducing the temperature of the primary combustion within the range of 950-1100 ℃.
When the temperature of the secondary flue gas is higher than 850-1000 ℃, reducing the temperature of the primary combustion within the range of 950-1100 ℃; reducing the temperature of secondary combustion within the range of 850-1000 ℃; the temperature of the secondary combustion is preferably reduced within the range of 850-1000 ℃ to reduce the temperature of the secondary flue gas to 850-1000 ℃, and when the temperature of the secondary flue gas is still higher than 850-1000 ℃, the temperature of the primary combustion is preferably reduced within the range of 950-1100 ℃.
In order to better understand the present invention, the following examples are further provided to illustrate the present invention, but the present invention is not limited to the following examples.
Example 1
As shown in the process flow of figure 1, 400 kg of straws are crushed and bundled and then enter a combustion chamber for downstream anoxic combustion, the excess air coefficient during the anoxic combustion is controlled by a fan to be preferably 0.8, the anoxic combustion temperature is 650 ℃, the time of single bundle anoxic combustion is 20min, and volatile gas is obtained, wherein the volatile gas comprises H2(the mass percentage is preferably 23%), CO (the mass percentage is preferably 23%), and CO2(the mass percentage is preferably 30%) and CH4(the mass percentage content is preferably 21%).
Sorting and dehydrating 1t of domestic garbage, and drying in a hopper at the drying temperature of 150 ℃ for 3h to obtain dried domestic garbage and dried flue gas.
And (3) allowing the dried household garbage to enter a pyrolysis chamber for oxygen-insulated pyrolysis, wherein the heating rate of the oxygen-insulated pyrolysis is 150 ℃/min, the temperature of the oxygen-insulated pyrolysis is preferably 900 ℃, and the time of the oxygen-insulated pyrolysis is 55min, so as to obtain pyrolysis gas.
The method comprises the steps of conveying pyrolysis gas to a primary combustion chamber through a pyrolysis gas pipeline in a hot cleaning furnace under the heat preservation condition, conveying volatile gas and dry flue gas to the primary combustion chamber through a flue gas pipeline, spraying out the volatile gas and the dry flue gas through a mixer nozzle in the primary combustion chamber to be mixed, wherein the mixer nozzle is circularly arranged, the mixed gas nozzle is sprayed in at a tangential angle of 5-10 degrees, initial flue gas is obtained to be subjected to cyclone primary combustion, the excess air coefficient during primary combustion is controlled to be 1.2 by spraying first air through a first air distribution nozzle in the primary combustion chamber, the oxygen content during primary combustion is 8%, the temperature of the primary combustion is 950 ℃, the time of the primary combustion is 2.5s, and the primary flue gas with the temperature of 950 ℃ is obtained.
Carry the one-level flue gas to the postcombustion chamber through flue gas channel, wherein, set up in the flue gas channel and keep off 3 and flow the board, realize that the one-level flue gas gets into the postcombustion chamber after 3 times baffling.
And after the primary flue gas enters the secondary combustion chamber, controlling the flow direction of second air sprayed by a second air distribution nozzle at the inlet of the secondary combustion chamber to be opposite to that of the primary flue gas, and performing disturbance secondary combustion, wherein the excess air coefficient during secondary combustion is 1, the temperature of the secondary combustion is 850 ℃, the oxygen content during secondary combustion is 10 percent, and the time of the secondary combustion is 1.5s, so as to obtain secondary flue gas with the temperature of 850 ℃.
And heating the domestic garbage during oxygen-isolated pyrolysis by using the secondary flue gas, heating the domestic garbage during drying by using the primary heat exchange flue gas after heat exchange to obtain the secondary heat exchange flue gas, and emptying.
The secondary flue gas obtained in the example 1 is sampled to be subjected to chromatographic detection, a suma tank is used for collecting the secondary flue gas, a gas chromatography-mass spectrometer is used for monitoring, the chromatographic detection result is shown in fig. 3 and can be obtained from the chromatographic result, the secondary flue gas contains ethylene, acetylene, ethane, propylene, acetaldehyde, methyl chloride, benzene, acetone, propanal and propane, dioxin is not contained, the mass percentage content of each component is shown in fig. 4 and table 1, and the combustion efficiency of the pyrolysis gas is 97.3%.
Table 1 example 1 secondary flue gas component content
Example 2
As shown in the process flow of figure 1, 700kg straws are crushed and bundled and then enter a combustion chamber for downstream anoxic combustion, the excess air coefficient during the anoxic combustion is controlled by a fan to be preferably 0.8, the anoxic combustion temperature is 750 ℃, the time of single bundle anoxic combustion is 20min, and volatile gas is obtained, wherein the volatile gas comprises H2(the mass percentage is preferably 23%), CO (the mass percentage is preferably 23%), and CO2(the mass percentage is preferably 30%) and CH4(the mass percentage is preferably 21%)。
And (3) sorting and dehydrating the 2t of domestic garbage, and drying in a hopper at the drying temperature of 200 ℃ for 2h to obtain dried domestic garbage and dried flue gas.
And (3) allowing the dried household garbage to enter a pyrolysis chamber for oxygen-insulated pyrolysis, wherein the heating rate of the oxygen-insulated pyrolysis is 200 ℃/min, the temperature of the oxygen-insulated pyrolysis is preferably 1000 ℃, and the time of the oxygen-insulated pyrolysis is 45min, so as to obtain pyrolysis gas.
The method comprises the steps of conveying pyrolysis gas to a primary combustion chamber through a pyrolysis gas pipeline in a hot cleaning furnace under the condition of heat preservation, conveying volatile gas and dry flue gas to the primary combustion chamber through a flue gas pipeline, spraying out the volatile gas and the dry flue gas through a mixer nozzle in the primary combustion chamber to be mixed, wherein the mixer nozzle is circularly arranged, the mixed gas nozzle is sprayed in at a tangential angle of 5-10 degrees, initial flue gas is obtained to be subjected to cyclone primary combustion, the excess air coefficient during primary combustion is controlled to be 1.3 through a first air distribution nozzle in the primary combustion chamber, the oxygen content during primary combustion is 13%, the temperature of the primary combustion is 1100 ℃, the time of the primary combustion is 2.5s, and the primary flue gas with the temperature of 1100 ℃ is obtained.
Carry the one-level flue gas to the postcombustion chamber through flue gas channel, wherein, set up in the flue gas channel and keep off 3 and flow the board, realize that the one-level flue gas gets into the postcombustion chamber after 3 times baffling.
And after the primary flue gas enters the secondary combustion chamber, controlling the flow direction of second air sprayed by a second air distribution nozzle at the inlet of the secondary combustion chamber to be opposite to that of the primary flue gas, and performing disturbance secondary combustion, wherein the excess air coefficient during secondary combustion is 1.2, the temperature of secondary combustion is 1000 ℃, the oxygen content during secondary combustion is 14 percent, and the time of secondary combustion is 1.5s, so as to obtain the secondary flue gas with the temperature of 1000 ℃.
And heating the domestic garbage during oxygen-isolated pyrolysis by using the secondary flue gas, heating the domestic garbage during drying by using the primary heat exchange flue gas after heat exchange to obtain the secondary heat exchange flue gas, and emptying.
And (3) sampling the secondary flue gas obtained in the embodiment 2 for chromatographic detection, collecting the secondary flue gas by using a Suma tank, and monitoring by using a gas chromatography-mass spectrometer, wherein the chromatographic detection result is similar to that in the embodiment 1, and the combustion efficiency of the pyrolysis gas is the same as that in the embodiment 1.
The foregoing is merely a preferred embodiment of the invention and is not intended to limit the invention in any manner. It should be noted that, for those skilled in the art, without departing from the principle of the present invention, several improvements and modifications can be made, and these improvements and modifications should also be construed as the protection scope of the present invention.

Claims (6)

1. A method for clean combustion of gas by using straw household garbage to cooperatively treat comprises the following steps:
carrying out anoxic combustion on the straws to obtain volatile gas;
carrying out oxygen-insulating pyrolysis on household garbage to obtain pyrolysis gas, wherein the temperature of the oxygen-insulating pyrolysis is 900-1000 ℃, the feeding amount of the household garbage is 950-1100 kg/h, the heating rate of the oxygen-insulating pyrolysis is 150-200 ℃/min, and the time of the oxygen-insulating pyrolysis is 35-60 min;
mixing the pyrolysis gas with the volatile gas after heat preservation to obtain initial flue gas, and performing primary combustion and secondary combustion on the initial flue gas to obtain secondary flue gas;
the temperature of the pyrolysis gas after heat preservation is 900-1000 ℃;
the temperature of the primary combustion is 950-1100 ℃, the oxygen content of the primary combustion is 8-13%, the excess air coefficient of the primary combustion is 1.2-1.3, the time of the primary combustion is 2-3 s, the temperature of the secondary combustion is 850-1000 ℃, the oxygen content of the secondary combustion is 10-14%, the excess air coefficient of the secondary combustion is 1-1.2, and the time of the secondary combustion is 1-2 s.
2. The method according to claim 1, wherein the excess air ratio in the anoxic combustion is 0.8 to 0.85, and the temperature of the anoxic combustion is 650 to 750 ℃.
3. The method of claim 1, wherein the volatile gas comprises H2、CO、CO2And CxHy
4. The method according to claim 1, further comprising drying the domestic waste before the oxygen-isolated pyrolysis, wherein the drying temperature is 150-200 ℃, and the drying time is 2-3 h.
5. The method according to claim 1, wherein after the secondary flue gas is obtained, the method further comprises heating the secondary flue gas when the secondary flue gas is used for the oxygen-isolated pyrolysis of the household garbage to obtain the heat exchange flue gas.
6. The method of claim 5, wherein after obtaining the heat exchange flue gas, the method further comprises heating the heat exchange flue gas when the heat exchange flue gas is used for drying the household garbage.
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