WO2022193537A1 - 封闭式负压固体废物控氧热解装置 - Google Patents

封闭式负压固体废物控氧热解装置 Download PDF

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WO2022193537A1
WO2022193537A1 PCT/CN2021/111945 CN2021111945W WO2022193537A1 WO 2022193537 A1 WO2022193537 A1 WO 2022193537A1 CN 2021111945 W CN2021111945 W CN 2021111945W WO 2022193537 A1 WO2022193537 A1 WO 2022193537A1
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pyrolysis
burner
gas
outlet
inlet
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PCT/CN2021/111945
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English (en)
French (fr)
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徐健元
林建东
陈永基
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佛山市华洁源热能与环境工程技术有限公司
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Publication of WO2022193537A1 publication Critical patent/WO2022193537A1/zh

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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
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/14—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
    • 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
    • F23G5/442—Waste feed arrangements
    • F23G5/444—Waste feed arrangements for solid waste
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/50—Control or safety arrangements

Definitions

  • the invention relates to a solid waste pyrolysis device, in particular to an oxygen control pyrolysis device applied to solid waste reduction and harmless treatment and coordinated harmful gas treatment, belonging to the technical field of energy saving and environmental protection.
  • the traditional pyrolysis furnace is used to treat solid waste, although it produces less harmful components in the exhaust gas, but the pyrolysis rate is extremely low, which is not suitable for the treatment of solid waste with a large reduction.
  • the technical problem to be solved by the present invention is to design a solid waste pyrolysis device with low investment, high treatment efficiency, low operating cost and low secondary pollution, which can synergistically treat relevant harmful gases in the solid waste treatment process, greatly reducing the Exhaust gas purification costs, reduce environmental pollution, simplify the process flow, save energy consumption, improve safety and improve the working environment.
  • the present invention can take following technical scheme:
  • a closed negative pressure solid waste oxygen control pyrolysis device comprising a dryer, a pyrolysis burner, a low calorific value gas burner, a flue gas heat exchanger, a condensation dehumidifier, a hot air circulation fan, a pyrolysis gas exhaust fan and
  • the dryer is provided with a material inlet, a material outlet, a hot air inlet and a moisture outlet
  • the pyrolysis burner is provided with a material inlet, a slag outlet and a pyrolysis gas outlet
  • the gas burner is provided with an air inlet and a flue gas outlet
  • the flue gas heat exchanger is provided with a flue gas inlet, a tail gas outlet, a hot air outlet and a circulating return air outlet.
  • the inlet and outlet of the first heat exchange channel of the gas heat exchanger, the hot air outlet and the circulating air return port are respectively connected to the inlet and outlet of the second heat exchange channel of the flue gas heat exchanger;
  • the moisture outlet, condensing dehumidifier, hot air return port of flue gas heat exchanger, hot air outlet of flue gas heat exchanger, hot air circulation fan, and hot air inlet of dryer are connected in sequence through hot air circulation pipe to form a closed circulation structure ;
  • the pyrolysis gas outlet of the pyrolysis burner is connected with the air inlet of the low calorific value gas burner through the pyrolysis gas exhaust fan, the pyrolysis gas conveying pipe and the main fan, and the pyrolysis gas at the air inlet end of the main fan is connected.
  • the conveying pipe is connected with the hot air circulation pipe through the bypass pipe;
  • the flue gas outlet of the low calorific value gas burner is connected with the flue gas inlet of the flue gas heat exchanger;
  • the material outlet of the dryer is connected with the gas outlet of the pyrolysis burner.
  • the material inlets are connected through a material elevator, and the material elevator is located in the material conveying sealing area, and the material outlet of the dryer and the material inlet of the pyrolysis burner are connected through the material conveying sealing area;
  • the pyrolysis combustion A grate is arranged below the inside of the device, and a plurality of combustion-supporting air chambers are arranged below the grate from left to right.
  • the present invention can further take the following improvement measures to solve the problem:
  • a further improvement is that the dryer is provided with a continuous conveyor belt.
  • the grate is a single-layer grate, and one or more layers of conveyor belts are arranged above the grate.
  • the grate is a grate that can continuously pyrolyze and combust materials, and the grate is a reciprocating grate.
  • a further improvement is that the pyrolysis burner is provided with a burner.
  • a further improvement is that the combustion-supporting air chambers in the lower part of the pyrolysis burner are respectively communicated with the first combustion-supporting fan, the second combustion-supporting fan, and the third combustion-supporting fan;
  • the suction port of the second combustion-supporting fan is communicated with the hot air circulation pipe at the front end of the inlet of the condensing dehumidifier; or the branch pipe of the pyrolysis gas conveying pipe of the third combustion-supporting fan is communicated; External connection.
  • a further improvement is that the low calorific value gas burner is provided with a heat exchange area for heat exchange in the first air flow channel and the second air flow channel, and a combustion chamber; the inlet of the first air flow channel is connected to the low calorific value.
  • the air inlet of the gas burner, the outlet of the first air flow channel is connected to the combustion chamber, and the inlet of the second air flow channel is connected to the combustion chamber.
  • flue gas heat exchanger is a heat exchanger with two-way reverse airflow heat exchange, and the inlet of the first heat exchange channel of the flue gas heat exchanger is connected to the second heat exchanger of the low calorific value gas burner. The outlet of the airflow channel is communicated.
  • a further improvement is that the condensation dehumidifier is connected to the cooling water circulation pipeline of the cooling tower.
  • a further improvement is that the combustion chamber of the low calorific value gas burner is communicated with the grate area space of the pyrolysis burner through a refractory heat-insulating pipe.
  • the pyrolysis burner has the function of controlling the oxygen supply during the high temperature combustion and pyrolysis of materials.
  • the combustion efficiency of solid waste is higher than that of pyrolysis, the total amount of flue gas and harmful components generated by combustion are also more, which increases the difficulty and investment of exhaust gas purification, and secondary combustion of flue gas generated by combustion can effectively Decomposes most of the harmful components in the flue gas and greatly reduces the purification cost of the exhaust gas.
  • the exhaust gas mainly composed of nitrogen and carbon dioxide, a certain proportion of combustible gas needs to be added to achieve secondary combustion.
  • the present invention controls the ratio between material combustion and pyrolysis by controlling the oxygen supply in the solid waste pyrolysis process, and can generate an appropriate proportion of carbon monoxide and other combustible gases through oxygen-controlled pyrolysis while taking into account the solid waste treatment efficiency.
  • the secondary combustion of exhaust gas can meet the needs of efficiency, environmental protection and economy.
  • the low calorific value gas burner can conduct non-contact heat exchange between the combustible gas generated by pyrolysis and the high temperature flue gas in the process of entering the combustion chamber, and make full use of the heat of the high temperature flue gas after the combustion of the combustible gas to improve the combustible gas to be combusted. It can have the function of low concentration or low calorific value combustible gas combustion, so that only a small amount of combustible pyrolysis gas or a small amount of fuel is needed to realize spontaneous combustion of low calorific value combustible gas, so as to complete the secondary combustion purification of exhaust gas. If the above conditions are met, the pyrolysis ratio of solid waste should be reduced as much as possible, and the combustion ratio of solid waste should be increased to improve the efficiency of solid waste reduction.
  • the invention is suitable for the harmless and weight-reducing treatment of solid wastes with low calorific value.
  • the low calorific value of solid wastes including domestic sludge reaches 800Kcal/kg, high-efficiency combustion can be achieved and a sufficient amount of combustible pyrolysis can be produced at the same time.
  • the low calorific value gas burner can inhale more air from other places to participate in the secondary combustion of the exhaust gas without the need for additional supplementary fuel, including It can inhale the odorous moisture produced by the dryer and the air in the surrounding environment.
  • the invention has excellent energy-saving effect.
  • the pyrolysis combustible gas produced by incomplete combustion is finally involved in the mixed combustion of harmful gas, thereby reducing the cost of additional fuel for the secondary combustion of tail gas.
  • a certain proportion of pyrolysis gas combustion can reduce the total amount of exhaust emissions, reduce the loss of exhaust heat dissipation, and use the flue gas heat exchanger to recover the waste heat of the flue gas for the front drying of solid waste.
  • the calorific value is fully utilized.
  • Embodiment 1 is a schematic structural diagram of Embodiment 1 of the present invention.
  • FIG. 2 is a schematic structural diagram of the dryer according to Embodiment 1 of the present invention.
  • FIG. 3 is a schematic structural diagram of the pyrolysis burner according to Embodiment 1 of the present invention.
  • FIG. 4 is a schematic structural diagram of the low calorific value gas burner according to Embodiment 1 of the present invention.
  • FIG. 5 is a schematic structural diagram of a pyrolysis burner according to Embodiment 2 of the present invention.
  • FIG. 6 is a schematic structural diagram of Embodiment 3 of the present invention.
  • FIG. 7 is a schematic structural diagram of another embodiment of the present invention.
  • Embodiment 1 As shown in Figures 1 to 4, a closed negative pressure solid waste oxygen control pyrolysis device, comprising a dryer 1, a pyrolysis burner 2, a low calorific value gas burner 3, a flue gas heat exchange 4, condensation dehumidifier 5, hot air circulation fan 6, pyrolysis gas exhaust fan 7 and main fan 8, the dryer 1 is provided with a material inlet 13, a material outlet 14, a hot air inlet 11 and a moisture outlet 12 , the pyrolysis burner 2 is provided with a material inlet 23, a slag outlet 24 and a pyrolysis gas outlet 22, the low calorific value gas burner 3 is provided with an air inlet 31 and a flue gas outlet 34, the smoke The gas heat exchanger 4 is provided with a flue gas inlet 43, a tail gas outlet 44, a hot air outlet 42 and a circulating return air outlet 41.
  • the flue gas inlet 43 and the exhaust gas outlet 44 are respectively connected to the first heat exchange channel of the flue gas heat exchanger.
  • the inlet and outlet, the hot air outlet 42 and the circulating air outlet 41 are respectively connected to the inlet and outlet of the second heat exchange channel 45 of the flue gas heat exchanger; the moisture outlet 12,
  • the condensing dehumidifier 5, the hot air return port 41 of the flue gas heat exchanger 4, the hot air outlet 42 of the flue gas heat exchanger 4, the hot air circulation fan 6, and the hot air inlet 11 of the dryer 1 are sequentially connected through the hot air circulation pipe 56 to form a Closed circulation structure;
  • the pyrolysis gas outlet 22 of the pyrolysis burner 2 is connected to the air inlet 31 of the low calorific value gas burner 3 through the pyrolysis gas exhaust fan 7, the pyrolysis gas conveying pipe 78 and the main fan 8,
  • the pyrolysis gas conveying pipe 78 at the air inlet end of the main fan 8 is connected to the hot air circulation pipe 56
  • the dryer 1 is provided with a continuous conveyor belt 15 .
  • the pyrolysis burner 2 contains a chain belt 25 capable of conveying materials continuously.
  • the chain belt 25 for conveying material is composed of a two-layer structure, and the grate 26 is arranged below the chain belt 25 for conveying material.
  • a further improved embodiment is: the grate 26 is a grate 26 that can continuously pyrolyze and burn materials, and is a reciprocating grate.
  • a further improved embodiment is: the pyrolysis burner 2 is provided with a burner 27 .
  • a further improved embodiment is: the combustion-supporting air chamber 28 below the pyrolysis burner 2 is communicated with the first combustion-supporting fan 29 , the second combustion-supporting fan 292 , and the third combustion-supporting fan 293 respectively.
  • the suction port of the second combustion-supporting fan 292 is communicated with the hot air circulation pipe 56 at the front end of the inlet of the condensing dehumidifier 5; or the branch pipe 82 of the pyrolysis gas conveying pipe 78 of the third combustion-supporting fan 293 is communicated;
  • the conveying sealing area communicates with or communicates with the outside world (as shown in FIG. 7 , so that the first combustion-supporting fan 29 can use fresh air).
  • Each combustion-supporting fan can be selectively used when in use.
  • Each combustion-supporting fan can be a variable-frequency combustion-supporting fan.
  • a further improved embodiment is: as shown in FIG. 4 , the low calorific value gas burner 3 is provided with a heat exchange area for the first air flow channel 35 and the second air flow channel 36 for heat exchange, and a combustion chamber. 32; the inlet of the first air flow channel 35 is connected to the air inlet 31 of the low calorific value gas burner 3, the outlet of the first air flow channel 35 is connected to the combustion chamber 32, the inlet of the second air flow channel 36 is connected to the combustion chamber, and the low calorific value gas The air inlet 31 of the burner 3 communicates with the inlet of the first air flow channel 35; it is suitable for the combustion of low calorific value gas, and the combustion chamber 32 is provided with a burner 33.
  • a further improved embodiment is as follows: the flue gas heat exchanger 4 is a heat exchanger for two-way reverse airflow heat exchange, and the inlet of the first heat exchange channel of the flue gas heat exchanger is connected to the low calorific value gas burner 3 . The outlet of the second air flow channel 36 communicates with each other.
  • a further improved embodiment is: the condensation dehumidification
  • a further improved embodiment is: the condensation dehumidifier 5 is connected to the cooling water circulation pipeline of the cooling tower.
  • the focus of the present invention is the air flow organization and control in the process of pyrolysis and combustion of solid waste (including secondary combustion of tail gas), and its purpose is aimed at two aspects, one is to control gas leakage to prevent safety accidents and environmental pollution, and the other is to control combustion support Wind achieves ideal pyrolysis and combustion conditions.
  • the flue gas heat exchanger for reheating enter the flue gas heat exchanger for reheating, and then enter the dryer for continuous circulation, which can avoid the emission of harmful gases in the drying process, thus solving the pollution to the environment caused by the emission of harmful gases in the traditional drying and dehumidification process.
  • the single method of closed circulation cannot completely avoid the leakage of gas in the dryer. Since the drying of materials in the dryer requires hot air with a certain flow rate, there must be enough negative pressure in the dryer to avoid internal air leakage. The disturbed airflow leaks from the inlet and outlet of the material, and the volatilization of water in the material increases the amount of water vapor, so the exhaust air volume of the dryer must be much larger than the air intake volume.
  • the present invention passes the gas in the hot air circulation pipe through the bypass pipe.
  • Part of the main fan is introduced into the low calorific value gas burner for combustion support, so that the exhaust air volume in the dryer is greater than the intake air volume.
  • two methods of air closed-cycle dehumidification and dehydration and bypass ventilation are used to form negative pressure in the cavity.
  • a material conveying sealing area is set to relatively seal the area, which is equivalent to the material conveying sealing area being communicated with the interior of the dryer through the material outlet.
  • the rear is also a negative pressure space, but a fresh air inlet is reserved at the top of the material conveying sealing area, so that the odor emitted from the material on the material elevator will come down from the fresh air outlet and be inhaled from the outlet of the dryer.
  • the pyrolysis burner also has the problem of gas leakage.
  • the pyrolysis burner must also form a negative pressure inside to prevent the internal harmful gas from leaking from the material inlet and slag outlet.
  • the air outlet has sufficient exhaust air volume and exceeds the intake air volume of combustion air to ensure negative pressure in the pyrolysis burner.
  • All the gas generated by the pyrolysis burner and part of the gas generated by the dryer are sucked in by the main fan with a larger air volume than the pyrolysis gas exhaust fan and sent to the low calorific value gas burner for combustion.
  • the air flow is driven by the main fan at the air inlet end to form a positive pressure, and after combustion, it is discharged through the chimney 47 after passing through the flue gas heat exchanger and the rear-stage purifier 46 . Since the low calorific value gas burner has no material inlet and outlet, there is no possibility of gas leakage from other openings other than the exhaust gas outlet.
  • the dryer only dries the material initially, and then sends the material to the pyrolysis burner to complete the re-drying, pyrolysis, combustion, burning ember and slag discharge of the material.
  • the pyrolysis and incineration of solid waste are carried out on the grate of the pyrolysis burner.
  • the air intake of each combustion-supporting air chamber can be adjusted to control the air flow rate of the grate above it.
  • the combustion-supporting air volume obtained by the material during the pyrolysis or combustion process is used to control the working conditions of the pyrolysis section and the combustion section of the material respectively, so as to achieve the best pyrolysis and combustion ratio.
  • the combustion-supporting air in the pyrolysis and combustion section mainly comes from the combustion-supporting fan corresponding to the combustion-supporting air chamber below it.
  • the multiple combustion-supporting fans at the bottom of the grate of the pyrolysis burner can be selected to absorb the moist air in the hot air circulation pipe 56 at the front end of the inlet of the condensing dehumidifier 5 or the pyrolysis gas or fresh air from the branch pipe 82 of the pyrolysis gas conveying pipe 78. If Sending a small part of the pyrolysis gas into the combustion grate section for combustion support can properly supplement the heat required for the pyrolysis of the material and reduce the energy consumption of the burner.
  • the moisture generated by drying is sent to the combustion grate section for combustion support, Water vapor can be burned through hot coal to produce water gas, which is beneficial to improve combustion efficiency and flue gas quality.
  • a small amount of air inhaled from the negative pressure of the slag outlet is also regarded as a part of the combustion-supporting air. Since the slag outlet is close to the burning section of the grate, the slag burning almost consumes the oxygen in this part of the air, so it is The air sucked in by the slag port has little effect on the pyrolysis and combustion conditions.
  • the "pyrolysis” mentioned above belongs to the pyrolysis with oxygen participation, which means that the material can only support the complete combustion of part of the material due to the amount of oxygen at high temperature, and the other part of the material does not burn due to lack of oxygen but absorbs convection.
  • the high temperature flue gas heat or the heat radiated or conducted from nearby high temperature objects makes the organic matter in the material gasify to generate pyrolysis gas.
  • the moisture content of the solid waste to be treated is low, only a single layer of grate is required in the pyrolysis burner. If the moisture content of the solid waste is high, one or more layers of chain belts can be added above the grate for drying. Dry, use the heat of the internal flue gas to dry the moisture in the material on the chain belt.
  • the combustion part also includes the secondary combustion of the exhaust gas.
  • the combustion of this link is completed in the low calorific value gas burner.
  • the purpose of the exhaust gas secondary combustion is to mix and concentrate all the gases produced by the dryer and the pyrolysis burner for a round of combustion.
  • the harmful components of the exhaust gas will be greatly reduced.
  • the chimney 47 is discharged directly up to the standard. If the solid waste with high content such as sulfide, nitride or chloride is processed, it can be discharged up to the standard only by performing a corresponding simple purification treatment through the rear-stage purifier 46 .
  • the low calorific value gas burner can be suitable for the combustion of combustible gas with lower calorific value or low concentration without adding fuel or less, it can be suitable for the combustion of combustible gas with a wide concentration range.
  • the air-fuel ratio (ratio of combustion-supporting air to combustible gas) of combustible gases such as carbon monoxide and methane can be increased by more than 10 times compared with ordinary combustion.
  • the combustion-supporting air participates in the combustion, that is, by increasing the frequency of the main fan, it can not only ensure the combustion of the mixed gas components under the condition of saving combustion, but also extract a large amount of drying waste gas to participate in the combustion-supporting to realize the negative pressure of the equipment and pipelines and solve the exhaust gas leakage. question.
  • the low calorific value gas burner firstly mixes the pyrolysis gas, combustion-supporting air and other gases fully and uniformly before entering the combustion chamber for combustion.
  • the flue gas heat exchanger receives the high-temperature exhaust gas at about 200°C from the low calorific value gas burner, and conducts non-contact heat exchange with the circulating air of the dryer, so that the waste heat of the exhaust gas can be fully utilized for material drying and saving. Energy consumption, because the high temperature flue gas does not contact the circulating air of the dryer, the exhaust gas will not be polluted.
  • a tar condensation collector 71 needs to be installed on the pyrolysis gas conveying pipe 78 , the working principle of which is similar to that of the condensation dehumidifier 5 .
  • a relatively sealed slag collection area can be set up at the slag outlet of the pyrolysis burner, and the air penetrates the slag through a high-pressure fan to blow the rest of the heat inward. Better utilization of waste heat and cooling of slag.
  • Embodiment 2 (As shown in Figure 1, Figure 2, Figure 4, Figure 5) a closed negative pressure solid waste oxygen control pyrolysis device, comprising a dryer 1, a pyrolysis burner 2, a low calorific value gas burner 3 , flue gas heat exchanger 4, condensation dehumidifier 5, hot air circulation fan 6, pyrolysis gas exhaust fan 7 and main fan 8, the dryer 1 is provided with material inlet 13, material outlet 14, hot air inlet 11 and The wet gas outlet 12, the pyrolysis burner 2 is provided with a material inlet 23, a slag outlet 24 and a pyrolysis gas outlet 22, the low calorific value gas burner 3 is provided with an air inlet 31 and a flue gas outlet 34 , the flue gas heat exchanger 4 is provided with a flue gas inlet 43, a tail gas outlet 44, a hot air outlet 42 and a circulating return air outlet 41; the flue gas inlet 43 and the exhaust gas outlet 44 are respectively connected to the The inlet and outlet of the first heat exchange pipe, the hot air outlet 42
  • the hot air inlet 11 of 1 is connected to a closed circulation structure through the hot air circulation pipe 56 in sequence, and the pyrolysis gas outlet 22 of the pyrolysis burner 2 passes through the pyrolysis gas exhaust fan 7, the pyrolysis gas conveying pipe 78 and the main fan.
  • the pyrolysis burner 2 is connected with the air inlet 31 of the low calorific value gas burner 3, and the pyrolysis gas delivery pipe 78 at the air inlet end of the main fan 8 communicates with the hot air circulation pipe 56 through the bypass pipe 58;
  • the flue gas outlet 34 is connected to the flue gas inlet 43 of the flue gas heat exchanger 4; the material outlet 14 of the dryer 1 and the material inlet 23 of the pyrolysis burner 2 are connected through a material elevator 91, and the material is lifted.
  • the machine 91 is arranged in the material conveying sealing area 9 ; the material outlet 14 of the dryer 1 and the material inlet 23 of the pyrolysis burner 2 are communicated through the material conveying sealing area 9 .
  • the pyrolysis burner 2 is provided with a grate 26 below it, and a plurality of combustion-supporting air chambers 28 are arranged below the grate 26 from left to right.
  • the dryer 1 is provided with a continuous conveyor belt 15 .
  • the pyrolysis burner 2 contains a chain belt 25 that can continuously convey materials, which is composed of a two-layer structure.
  • a further improved embodiment is: the grate 26 is a grate 26 that can continuously pyrolyze and burn materials, and is a reciprocating grate.
  • a further improved embodiment is: the pyrolysis burner 2 is provided with a burner 27 .
  • a further improved embodiment is: the combustion-supporting air chamber 28 below the pyrolysis burner 2 is communicated with the first combustion-supporting fan 29 , the second combustion-supporting fan 292 , and the third combustion-supporting fan 293 respectively.
  • a further improved embodiment is: the suction port of the second combustion-supporting fan 292 is communicated with the hot air circulation pipe 56 at the front end of the inlet of the condensation dehumidifier 5; or the branch pipe 82 of the pyrolysis gas conveying pipe 78 of the third combustion-supporting fan 293 is communicated;
  • the first combustion-supporting fan 29 communicates with the material conveying sealing area or communicates with the outside world.
  • Each combustion-supporting fan can be a variable-frequency combustion-supporting fan.
  • a further improved embodiment is: as shown in FIG. 4 , the low calorific value gas burner 3 is provided with a heat exchange area for the first air flow channel 35 and the second air flow channel 36 for heat exchange, and a combustion chamber. 32; the inlet of the first air flow channel 35 is connected to the air inlet 31 of the low calorific value gas burner 3, the outlet of the first air flow channel 35 is connected to the combustion chamber 32, the inlet of the second air flow channel 36 is connected to the combustion chamber, and the low calorific value gas The air inlet 31 of the burner 3 communicates with the inlet of the first air flow channel 35; it is suitable for the combustion of low calorific value gas, and the combustion chamber 32 is provided with a burner 33.
  • a further improved embodiment is as follows: the flue gas heat exchanger 4 is a heat exchanger for two-way reverse airflow heat exchange, and the inlet of the first heat exchange channel of the flue gas heat exchanger is connected to the low calorific value gas burner 3 . The outlet of the second air flow channel 36 communicates with each other.
  • a further improved embodiment is: the condensation dehumidifier 5 is connected to the cooling water circulation pipeline of the cooling tower.
  • Embodiment 3 (as shown in Figure 2, Figure 3, Figure 4, Figure 6) a closed negative pressure solid waste oxygen control pyrolysis device, comprising a dryer 1, a pyrolysis burner 2, a low calorific value gas burner 3 , flue gas heat exchanger 4, condensation dehumidifier 5, hot air circulation fan 6, pyrolysis gas exhaust fan 7 and main fan 8, the dryer 1 is provided with material inlet 13, material outlet 14, hot air inlet 11 and Wet gas outlet 12, the pyrolysis burner 2 is provided with a material inlet 23, a slag outlet 24 and a pyrolysis gas outlet 22, the low calorific value gas burner 3 is provided with an air inlet 31 and a flue gas outlet 34 , the flue gas heat exchanger 4 is provided with a flue gas inlet 43, a tail gas outlet 44, a hot air outlet 42 and a circulating return air outlet 41; the flue gas inlet 43 and the exhaust gas outlet 44 are respectively connected to the The inlet and outlet of the first heat exchange channel, the hot air outlet 42 and
  • the hot air inlet 11 of 1 is connected to a closed circulation structure through the hot air circulation pipe 56 in sequence, and the pyrolysis gas outlet 22 of the pyrolysis burner 2 passes through the pyrolysis gas exhaust fan 7, the pyrolysis gas conveying pipe 78 and the main fan.
  • the flue gas outlet 34 is connected to the flue gas inlet 43 of the flue gas heat exchanger 4; the material outlet 14 of the dryer 1 and the material inlet 23 of the pyrolysis burner 2 are connected through a material elevator 91, and the material is lifted.
  • the machine 91 is set in the material conveying sealing area 9; the material outlet 14 of the dryer 1 and the material inlet 23 of the pyrolysis burner 2 are communicated through the material conveying sealing area.
  • the pyrolysis burner 2 is provided with a grate 26 below it.
  • the combustion chamber 32 of the low calorific value gas burner 3 communicates with the area space of the grate 26 of the pyrolysis burner 2 through a refractory and heat-insulating pipe 10 .
  • the dryer 1 is provided with a continuous conveyor belt 15 .
  • the pyrolysis burner 2 contains a chain belt 25 and a grate 26 that can continuously convey materials, and is composed of a three-layer structure.
  • the grate 26 is provided below the pyrolysis burner 2 .
  • the grate 26 is a grate 26 that can continuously pyrolyze and combust materials, and the grate 26 is a reciprocating grate.
  • a further improved embodiment is: as shown in FIG. 4 , the low calorific value gas burner 3 is provided with a heat exchange area for the first air flow channel 35 and the second air flow channel 36 for heat exchange, and a combustion chamber. 32; the inlet of the first air flow channel 35 is connected to the air inlet 31 of the low calorific value gas burner 3, the outlet of the first air flow channel 35 is connected to the combustion chamber 32, the inlet of the second air flow channel 36 is connected to the combustion chamber, and the low calorific value gas The air inlet 31 of the burner 3 communicates with the inlet of the first air flow channel 35; it is suitable for the combustion of low calorific value gas, and the combustion chamber 32 is provided with a burner 33.
  • a further improved embodiment is as follows: the flue gas heat exchanger 4 is a heat exchanger for two-way reverse airflow heat exchange, and the inlet of the first heat exchange channel of the flue gas heat exchanger is connected to the low calorific value gas burner. The outlet of the second air flow channel 36 of 3 communicates with each other.
  • a further improved embodiment is: a further improved embodiment of the condensation dehumidification is: the condensation dehumidifier 5 is connected to the cooling water circulation pipeline of the cooling tower.
  • Example 3 is suitable for high-efficiency carbonization treatment of solid wastes with high carbon content.
  • Part of the flue gas is drawn from the combustion chamber of the low calorific value burner through the pipeline and enters the area near the grate of the combustion pyrolyzer.
  • the temperature is extremely high (about 850°C) but the oxygen content is low, and the proportion of the material burning after entering the pyrolysis burner is low.
  • the high temperature and low oxygen air directly contacts the material with high heating efficiency, which can quickly pyrolyze and gasify the organic matter in it. .
  • the grate does not need to provide combustion-supporting air at the bottom of the grate during operation (the basic design of Embodiment 1 can be used but the combustion-supporting fan is turned off during use), and the heat energy of low-oxygen and high-temperature flue gas is used to replace the heat energy of material combustion.
  • the slag produced will retain more carbon components, and the resource utilization value of the slag will be higher.
  • the invention is suitable for the pyrolysis and combustion treatment of solid wastes such as garbage and sludge, and for making charcoal by using greening garbage and agricultural product straws.

Abstract

本发明公开了一种封闭式负压固体废物控氧热解装置，包括烘干器、热解燃烧器、低热值气体燃烧器、烟气换热器、冷凝除湿器、热风循环风机、热解气抽风机和主风机，热解燃烧器的热解气出口通过热解气抽风机、热解气输送管和主风机与低热值气体燃烧器的进风口连接，所述的主风机进风口端的热解气输送管通过旁通管道连通热风循环管；所述的低热值气体燃烧器的烟气出口与烟气换热器的烟气进口连接；物料提升机设于物料输送密封区内。本发明可满足效率、环保和经济方面的需求。提高其燃烧比例可提高固废减量的效率。大大改善了作业环境，通过烟气换热器对烟气余热的回收用于固体废物的前段烘干，热值得到充分利用。

Description

封闭式负压固体废物控氧热解装置 技术领域
本发明涉及的是一种固体废物热解装置，具体涉及一种应用于固体废物减量化和无害化处理并协同有害气体处理的控氧热解装置，属于节能与环保技术领域。
背景技术
垃圾和污泥等固体废物的处置已成为当前政府的棘手问题，之前普遍采用的填埋处置方式只是将污染物转移并没有从根本上解决问题，废物填埋会造成土壤、地下水和周围空气的污染，而现有大型垃圾焚烧厂已无法满足目前不断增长的巨量垃圾处理需求。再有，因城市发展，很多地方的城市建设已经延伸到多年前的垃圾填埋区，如果不对之前填埋地下的垃圾清理，由垃圾发酵散发出来的有害气体会对周边居民的健康造成危害，在现时垃圾焚烧厂满负载的情况下，陈旧垃圾的处置难以找到出路。
在垃圾收集地附近建立分散式的中小型垃圾焚烧点，可以减少垃圾中转和运输带来的二次污染并减轻成本，也大大缓解了大型垃圾焚烧厂的负担，这是未来垃圾处置的方向。但建设数目众多的中小型垃圾焚烧项目会受资金的限制，对垃圾焚烧的排放物处理的手段和设施就难以采用大型垃圾焚烧厂的做法，而中小型垃圾焚烧点可能更靠近民居，因此采用低成本技术以减少垃圾焚烧时产生的二次污染是必须解决的问题。
之前有小型垃圾焚烧技术和设备出现，但这类设备普遍存在尾气污染物严重超标，需要很大的投资对尾气进行净化处理，造成设备投资大、运营费用高和处理环节复杂等一系列问题。而对于经过压滤后含水量尚高的低热值的生活污泥进一步无害化减量处理，目前的小型焚烧设备更无能为力。
而采用传统的热解炉处理固体废物，虽然其产生的尾气有害成分较少，但存在热解速度极低，不适用于大幅度减量的固体废物处理。
发明内容
本发明需要解决的技术问题是设计出一种投资少、处理效率高、 运行费用低和二次污染少的固体废物热解装置，可在固体废物处理过程中将相关有害气体协同处理，大幅降低尾气净化成本，减少环境污染，并使工艺流程简化、节省能源消耗、提高安全性以及改善作业环境。
本发明可以采取如下技术方案:
一种封闭式负压固体废物控氧热解装置，包括烘干器、热解燃烧器、低热值气体燃烧器、烟气换热器、冷凝除湿器、热风循环风机、热解气抽风机和主风机，所述的烘干器设有物料进口、物料出口、热风进口和湿气排口，所述的热解燃烧器设有物料进口、出渣口和热解气出口，所述的低热值气体燃烧器设有进风口和烟气出口，所述的烟气换热器设有烟气进口、尾气出口、热风出口和循环回风口，烟气进口、尾气出口分别对应连通于所述烟气换热器的第一换热通道的进口、出口，热风出口和循环回风口分别对应连通于所述烟气换热器的第二换热通道的进口、出口；所述的烘干器的湿气排口、冷凝除湿器、烟气换热器的热风回口、烟气换热器的热风出口、热风循环风机、烘干器的热风进口依序通过热风循环管连接成闭式循环结构；所述的热解燃烧器的热解气出口通过热解气抽风机、热解气输送管和主风机与低热值气体燃烧器的进风口连接，所述的主风机进风口端的热解气输送管通过旁通管道连通热风循环管；所述的低热值气体燃烧器的烟气出口与烟气换热器的烟气进口连接；所述的烘干器的物料出口与热解燃烧器的物料入口之间通过物料提升机连接，物料提升机设于物料输送密封区内，烘干器的物料出口与热解燃烧器的物料入口之间通过物料输送密封区连通；所述的热解燃烧器其内的下方设有炉排，炉排下方从左到右设有多个助燃风室。
本发明解决问题还可以进一步采取以下改进措施：
进一步的改进为，所述的烘干器内设有连续输送带。
进一步的改进为，炉排为单层炉排，炉排上方设有一层或多层输送物料链带。进一步的改进为，炉排是可连续热解和燃烧物料的炉排，炉排是往复式炉排。
进一步的改进为，所述的热解燃烧器设有燃烧器。
进一步的改进为，所述的热解燃烧器其内下方的助燃风室分别与第一助燃风机、第二助燃风机、第三助燃风机连通；
所述的第二助燃风机其吸风口与冷凝除湿器入口前端的热风循环管连通；或第三助燃风机热解气输送管的分支管连通；第一助燃风机与物料输送密封区内连通或与外界连通。
进一步的改进为，所述的低热值气体燃烧器内设有用于第一路气流通道、第二路气流通道进行换热的换热区，以及燃烧室；第一路气流通道的入口连通低热值气体燃烧器的进风口，第一路气流通道的出口连通燃烧室，第二路气流通道的入口连通燃烧室。
进一步的改进为，所述的烟气换热器为两路逆向气流换热的热交换器，所述烟气换热器的第一换热通道的入口与低热值气体燃烧器的第二路气流通道的出口连通。
进一步的改进为，所述的冷凝除湿器与冷却塔的冷却水循环管路连接。
进一步的改进为，所述的低热值气体燃烧器其燃烧室与所述的热解燃烧器的炉排区域空间通过耐火隔热管道连通。
上述技术方案具有这样的技术效果:
热解燃烧器具有在物料高温燃烧和热解过程中对供氧量控制的功能。虽然固体废物的燃烧效率高于热解效率，但燃烧产生的烟气总量和有害成分也较多，加大了尾气净化的难度和投入，而对燃烧产生的烟气进行二次燃烧可以有效分解烟气中绝大部分的有害成分，大幅减少尾气的净化成本，但对燃烧产生以氮气和二氧化碳为主的尾气需要加入一定比例的可燃气体才能实现二次燃烧。本发明通过控制固体废物热解过程中的供氧量来控制物料燃烧和热解之间的比例，可在兼顾固体废处理效率的同时，通过控氧热解产生适量比例的一氧化碳等可燃气体用于尾气的二次燃烧，可满足效率、环保和经济方面的需求。
低热值气体燃烧器可对热解产生的可燃性气体在进入燃烧室的过程中和高温烟气进行非接触的换热，充分利用可燃气体燃烧后的高温烟气的热量提升待燃烧的可燃气体的温度，可具备低浓度或低热值可燃气体燃烧的功能，这样只需少量可燃热解气或补充少量燃燃料的情况下实现低热值可燃气体实现自燃，以完成尾气的二次燃烧净化，在满足上述条件下尽量降低固体废物的热解比例，提高其燃烧比例可提高固废减量的效率。
本发明适用于较低热值的固体废物无害化减量处理，包括生活污泥在内的固体废物，其低位热值达到800Kcal/kg时可实现高效燃烧并同时产生足量的可燃热解气满足尾气自燃所需要的热量，如果固体废物的低位热值有所增加，低热值气体燃烧器可在不需要额外补充燃料的条件下吸入更多来自其他地方的空气参与尾气二次燃烧，包括可以吸入烘干器产生的带异味的湿气和周围环境中的空气，如果将烘干器、热解燃烧器、物料提升机的封闭区及相关管道内部空气抽取参与尾气的二次燃烧，这样将对上述所有设备及管道内部形成负压，固体废物在整个处理过程所产生的有害气体就无法泄漏，大大改善了作业环境，对于防止有毒热解气的外泄尤其重要。
本发明具有优良的节能效果，一方面对未能完全燃烧产生的热解可燃气体最后参与有害气体混合燃烧，减少了尾气二次燃烧的外加燃料成本。再有，一定比例的热解气燃烧可以减少尾气排放总排量，降低尾气散热损失，并通过烟气换热器对烟气余热的回收用于固体废物的前段烘干，固体废物中原有的热值得到充分利用。
附图说明
附图1是本发明实施例1的结构示意图。
附图2是本发明实施例1的烘干器的结构示意图。
附图3是本发明实施例1的热解燃烧器的结构示意图。
附图4是本发明实施例1的低热值气体燃烧器的结构示意图。
附图5是本发明实施例2的热解燃烧器的结构示意图。
附图6是本发明实施例3的结构示意图。
附图7是本发明另一种实施例的结构示意图。
具体实施方式
下面结合具体实施例对本发明进行具体描述。
实施例1：如图1至图4所示，一种封闭式负压固体废物控氧热解装置，包括烘干器1、热解燃烧器2、低热值气体燃烧器3、烟气换热器4、冷凝除湿器5、热风循环风机6、热解气抽风机7和主风机8，所述的烘干器1设有物料进口13、物料出口14、热风进口11和湿气排口12，所述的热解燃烧器2设有物料进口23、出渣口24和 热解气出口22，所述的低热值气体燃烧器3设有进风口31和烟气出口34，所述的烟气换热器4设有烟气进口43、尾气出口44、热风出口42和循环回风口41，烟气进口43、尾气出口44分别对应连通于所述烟气换热器的第一换热通道的进口、出口，热风出口42和循环回风口41分别对应连通于所述烟气换热器的第二换热通道45的进口、出口；所述的烘干器1的湿气排口12、冷凝除湿器5、烟气换热器4的热风回口41、烟气换热器4的热风出口42、热风循环风机6、烘干器1的热风进口11依序通过热风循环管56连接成闭式循环结构；所述的热解燃烧器2的热解气出口22通过热解气抽风机7、热解气输送管78和主风机8与低热值气体燃烧器3的进风口31连接，所述的主风机8进风口端的热解气输送管78通过旁通管道58连通热风循环管56；所述的低热值气体燃烧器3的烟气出口34与烟气换热器4的烟气进口43连接；所述的烘干器1的物料出口14与热解燃烧器2的物料入口23之间通过物料提升机91连接，物料提升机91设于物料输送密封区9内，烘干器1的物料出口14与热解燃烧器2的物料入口23之间通过物料输送密封区9连通；所述的热解燃烧器2其内的下方设有炉排26，炉排26下方从左到右设有多个助燃风室28。
所述的烘干器1内设有连续输送带15。
所述的热解燃烧器2其内含有可连续输送物料链带25，输送物料链带25是二层结构组成，炉排26设于输送物料链带25下方。
进一步的改进实施例为：所述炉排26是可连续热解和燃烧物料的炉排26，是往复式炉排。
进一步的改进实施例为：所述的热解燃烧器2设有燃烧器27。
进一步的改进实施例为：所述的热解燃烧器2其内下方的助燃风室28分别与第一助燃风机29、第二助燃风机292、第三助燃风机293连通。
所述的第二助燃风机292其吸风口与冷凝除湿器5入口前端的热风循环管56连通；或第三助燃风机293热解气输送管78的分支管82连通；第一助燃风机29与物料输送密封区内连通或与外界连通(如图7所示，这样第一助燃风机29可以使用新风)。使用时各个助燃风机可以选择性使用。各个助燃风机可以为变频助燃风机。
进一步的改进实施例为：如图4所示，所述的低热值气体燃烧器 3内设有用于第一路气流通道35、第二路气流通道36进行换热的换热区，以及燃烧室32；第一路气流通道35的入口连通低热值气体燃烧器3的进风口31，第一路气流通道35的出口连通燃烧室32，第二路气流通道36的入口连通燃烧室，低热值气体燃烧器3的进风口31与第一路气流通道35的入口连通；适用于低热值燃气的燃烧，所述的燃烧室32设有燃烧机33。
进一步的改进实施例为：所述的烟气换热器4为两路逆向气流换热的热交换器，所述烟气换热器的第一换热通道的入口与低热值气体燃烧器3的第二路气流通道36的出口连通。
进一步的改进实施例为：所述的冷凝除湿
进一步的改进实施例为：所述的冷凝除湿器5与冷却塔的冷却水循环管路连接。
工作原理：
本发明的重点是对于固体废物的热解和燃烧(包括尾气二次燃烧)过程中的气流组织与控制，其目的针对两方面，一是控制气体泄漏防止安全事故和环境污染，二是控制助燃风实现理想的热解与燃烧工况。
在控制气体泄漏方面，由于设备存在多个物料进出口，也包括设备和管道存在密封不良的可能性，因此很容易在运行过程中出现有害气体泄漏，在保证符合工艺要求的运行工况前提下，减少有害气体的产生量，控制敏感段的设备和管道内部保持足够的负压是关键所在。在烘干段采用闭式循环风除湿的烘干脱水方式，烘干所产生湿臭气体不需要对外排放，通过冷凝除湿器对烘干器排出的高湿度的循环风进行冷凝除湿，空气除湿后再进入烟气换热器重新加热后再进入烘干器不断循环，这样可以避免烘干环节对外排放有害气体，以此解决了传统烘干排湿过程伴随有害气体的排放对环境带来污染。但是，只是采用闭式循环的单一手段还不能完全避免烘干器内气体的泄漏，由于对烘干器内物料烘干需要一定流速的热风，烘干器内必须有足够的负压才能避免内部扰动气流从物料进出口外泄，再加上物料中的水分挥发增加了水蒸气量，就必须让烘干器的排风量远大于进风量，本发明将热风循环管内的气体通过旁通管道部分引入主风机送入低热值气体燃烧器内用于助燃，以此实现烘干器内排风量大于进风量。上述在烘 干环节防止气体泄漏方面，采用了空气闭式循环除湿脱水和旁路抽风形成腔内负压两种手段双管齐下。
由于物料从烘干器至热解燃烧器的输送过程中也会散发异味，因此设置了物料输送密封区对该区域也进行相对密封，相当于物料输送密封区通过物料出口与烘干器内部连通后也同属一个负压空间，但在物料输送密封区的顶部保留一个新风入风口，这样从物料提升机上物料散发的气味会沿新风口下来从烘干器的出料口吸入。
热解燃烧器也同样存在气体泄漏的问题，热解燃烧器也必须让其内部形成负压才能防止内部有害气体从物料进口和出渣口外泄，其手段是利用热解气抽风机从热解气出口有足够的抽风量并超过助燃风的进风量以保证热解燃烧器内呈负压。
热解燃烧器产生的全部气体和烘干器产生的部分气体，通过比热解气抽风机更大抽风量的主风机吸入并送进低热值气体燃烧器进行燃烧，由于低热值气体燃烧器内气流由其进风口端的主风机驱动而呈正压，在燃烧后经烟气换热器和后级净化器46后通过烟囱47排放。由于低热值气体燃烧器不存在物料进出口，所以没有除尾气出口以外的其他开口泄漏气体的可能性。
上述所描述的是有害气体泄漏的原因以及解决方法，下面将对固体废物的热解、燃烧以及尾气二次燃烧通过控制助燃氧气实现符合工艺要求的工况作说明。
烘干器只是把物料进行初步烘干，然后将物料送入热解燃烧器完成物料的再次烘干、热解、燃烧、燃烬及渣料排出。
固体废物的热解和焚烧都在热解燃烧器炉排上进行，炉排下方从左到右设有多个助燃风室，可通过调整各个助燃风室的进风量来控制其上方炉排的物料在热解或燃烧过程获得的助燃风量，以此来分别控制物料的热解段和燃烧段的工况，实现最佳的热解和燃烧比例。热解和燃烧段的助燃风主要来自于其下方的助燃风室对应的助燃风机送风，只要控制助燃风机频率，就可以控制炉排上物料热解和燃烧的工况。热解燃烧器炉排底部的多个助燃风机，可以选择吸取冷凝除湿器5入口前端的热风循环管56中的湿空气或热解气输送管78的分支管82的热解气或新风，如果把小部分热解气送入燃烬炉排段助燃，可以适当补充物料的热解所需的热量而减少燃烧机的能耗，如果把烘干 产生的湿气送人燃烧炉排段助燃，水蒸气可以通过炽热的火炭产生水煤气燃烧有利于改善燃烧效率和烟气质量。另外，有少量从出渣口负压吸入的空气也视为助燃风的一部分，由于出渣口靠近炉排的燃烬段，炉渣燃烬也几乎消耗了这部分空气的氧分，所以从出渣口吸入的空气对于热解和燃烧工况影响不大。
上述所提及的“热解”属于有氧气参与的热解，指的是物料在高温下因氧气量只能支持其中部分物料的完全燃烧，另一部分物料因缺氧不产生燃烧但吸收了对流的高温烟气热量或从附近高温物体辐射或传导过来的热量使物料中的有机物气化产生热解气的过程。
如果被处理的固体废物含水量较低，热解燃烧器内只需要单一层炉排就可以，如果固体废物的含水量较高，可以在炉排上方增设一层或多层链带用于烘干，利用内部烟气热量烘干链带上物料中的水分。
燃烧部分还包括尾气的二次燃烧，该环节的燃烧在低热值气体燃烧器内完成，尾气二次燃烧其目的是将烘干器和热解燃烧器产生的气体全部混合集中再进行一轮燃烧以分解其中绝大部分的大分子物质，尾气的有害成分将大幅降低，对于处理某些有害成分较低的固体废物(如城市生活污泥)，在完成该燃烧环节或再经过除尘就可以从烟囱47直接达标排放，如果处理硫化物、氮化物或氯化物等含量较高的固体废物，只需要通过后级净化器46做相应简单的净化处理就可以达标排放。
由于低热值气体燃烧器可在不添加或少添加燃料的情况下适用于较低热值或较低浓度的可燃气体的燃烧，可适合浓度范围很大的可燃气体燃烧，本发明对于热解气中的一氧化碳和甲烷等可燃气体燃烧的空燃比(助燃空气与可燃气体的比率)可比普通燃烧提高10倍以上，所以，对于完全燃烧从热解燃烧器产生的热解气，可以混入大比例范围助燃空气参与燃烧，也就是通过加大主风机的频率，既可保证在节省燃烧的情况下对混合气体成分燃烧，也同时大量抽取烘干废气参与助燃实现设备和管道的负压而解决废气泄漏问题。低热值气体燃烧器是先把热解气、助燃空气及其它气体先充分均匀混合后再进入燃烧室燃烧，属于可燃气体全预混燃烧技术，具有燃烧充分和节能的效果。
烟气换热器是接收来自于低热值气体燃烧器排出的约200℃的高 温尾气，并将其与烘干器的循环风进行非接触换热，使尾气余热充分利用于物料烘干而节约能耗，由于高温烟气与烘干器的循环风没有产生接触，尾气不会受到污染。
如果处理木质素较高的固体废物，需要在热解气输送管78上加装焦油冷凝收集器71，其工作原理跟冷凝除湿器5类似。
如果处理热值较低的固体废物，为充分利用热能，可以在热解燃烧器出渣口处设置一个相对密封炉渣收集区，通过高压风机使空气穿透炉渣将其余热往里吹送，这样可以更充分利用余热并冷却炉渣。
实施例2：(如图1、图2、图4、图5)一种封闭式负压固体废物控氧热解装置，包括烘干器1、热解燃烧器2、低热值气体燃烧器3、烟气换热器4、冷凝除湿器5、热风循环风机6、热解气抽风机7和主风机8，所述的烘干器1设有物料进口13、物料出口14、热风进口11和湿气排口12，所述的热解燃烧器2设有物料进口23、出渣口24和热解气出口22，所述的低热值气体燃烧器3设有进风口31和烟气出口34，所述的烟气换热器4设有烟气进口43、尾气出口44、热风出口42和循环回风口41；烟气进口43、尾气出口44分别对应连通于所述烟气换热器的第一换热管道的进口、出口，热风出口42和循环回风口41分别对应连通于所述烟气换热器的第二换热管道45的进口、出口。
所述的烘干器1的湿气排口12、冷凝除湿器5、烟气换热器4的热风回口41、烟气换热器4的热风出口42、热风循环风机6、烘干器1的热风进口11依序通过热风循环管56连接成闭式循环结构，所述的热解燃烧器2的热解气出口22通过热解气抽风机7、热解气输送管78和主风机8与低热值气体燃烧器3的进风口31连接，所述的主风机8进风口端的热解气输送管78通过旁通管道58连通热风循环管56；所述的低热值气体燃烧器3的烟气出口34与烟气换热器4的烟气进口43连接；所述的烘干器1的物料出口14与热解燃烧器2的物料入口23之间通过物料提升机91连接，物料提升机91设于物料输送密封区9内；烘干器1的物料出口14与热解燃烧器2的物料入口23之间通过物料输送密封区9连通。所述的热解燃烧器2其内下方设有炉排26，炉排26下方从左到右设有多个助燃风室28。
所述的烘干器1内设有连续输送带15。
如图5所示，所述的热解燃烧器2内含有可连续输送物料链带25，是2层结构组成，炉排26设于输送物料链带25的右下方.
进一步的改进实施例为：炉排26是可连续热解和燃烧物料的炉排26，是往复式炉排。
进一步的改进实施例为：所述的热解燃烧器2设有燃烧器27。
进一步的改进实施例为：所述的热解燃烧器2其内下方的助燃风室28分别与第一助燃风机29、第二助燃风机292、第三助燃风机293连通。
进一步的改进实施例为：所述的第二助燃风机292其吸风口与冷凝除湿器5入口前端的热风循环管56连通；或第三助燃风机293热解气输送管78的分支管82连通；第一助燃风机29与物料输送密封区内连通或与外界连通。
各个助燃风机可以为变频助燃风机。
进一步的改进实施例为：如图4所示，所述的低热值气体燃烧器3内设有用于第一路气流通道35、第二路气流通道36进行换热的换热区，以及燃烧室32；第一路气流通道35的入口连通低热值气体燃烧器3的进风口31，第一路气流通道35的出口连通燃烧室32，第二路气流通道36的入口连通燃烧室，低热值气体燃烧器3的进风口31与第一路气流通道35的入口连通；适用于低热值燃气的燃烧，所述的燃烧室32设有燃烧机33。
进一步的改进实施例为：所述的烟气换热器4为两路逆向气流换热的热交换器，所述烟气换热器的第一换热通道的入口与低热值气体燃烧器3的第二路气流通道36的出口连通。
进一步的改进实施例为：所述的冷凝除湿器5与冷却塔的冷却水循环管路连接。
实施例3：(如图2、图3、图4、图6)一种封闭式负压固体废物控氧热解装置，包括烘干器1、热解燃烧器2、低热值气体燃烧器3、烟气换热器4、冷凝除湿器5、热风循环风机6、热解气抽风机7和主风机8，所述的烘干器1设有物料进口13、物料出口14、热风进口11和湿气排口12，所述的热解燃烧器2设有物料进口23、出渣口24和热解气出口22，所述的低热值气体燃烧器3设有进风口31 和烟气出口34，所述的烟气换热器4设有烟气进口43、尾气出口44、热风出口42和循环回风口41；烟气进口43、尾气出口44分别对应连通于所述烟气换热器的第一换热通道的进口、出口，热风出口42和循环回风口41分别对应连通于所述烟气换热器的第二换热通道45的进口、出口。
所述的烘干器1的湿气排口12、冷凝除湿器5、烟气换热器4的热风回口41、烟气换热器4的热风出口42、热风循环风机6、烘干器1的热风进口11依序通过热风循环管56连接成闭式循环结构，所述的热解燃烧器2的热解气出口22通过热解气抽风机7、热解气输送管78和主风机8与低热值气体燃烧器3的进风口31连接，所述的主风机8进风口端的热解气输送管78通过旁通管道58连通热风循环管56；所述的低热值气体燃烧器3的烟气出口34与烟气换热器4的烟气进口43连接；所述的烘干器1的物料出口14与热解燃烧器2的物料入口23之间通过物料提升机91连接，物料提升机91设于物料输送密封区9内；烘干器1的物料出口14与热解燃烧器2的物料入口23之间通过物料输送密封区连通。所述的热解燃烧器2其内下方设有炉排26。
如图6所示，所述的低热值气体燃烧器3其燃烧室32与所述的热解燃烧器2的炉排26区域空间通过耐火隔热管道10连通。
所述的烘干器1内设有连续输送带15。
所述的热解燃烧器2内含有可连续输送物料链带25和炉排26，是3层结构组成。炉排26设于热解燃烧器2下方。
炉排26是可连续热解和燃烧物料的炉排26，炉排26是往复式炉排。
进一步的改进实施例为：如图4所示，所述的低热值气体燃烧器3内设有用于第一路气流通道35、第二路气流通道36进行换热的换热区，以及燃烧室32；第一路气流通道35的入口连通低热值气体燃烧器3的进风口31，第一路气流通道35的出口连通燃烧室32，第二路气流通道36的入口连通燃烧室，低热值气体燃烧器3的进风口31与第一路气流通道35的入口连通；适用于低热值燃气的燃烧，所述的燃烧室32设有燃烧机33。
进一步的改进实施例为：所述的烟气换热器4为两路逆向气流换 热的热交换器，所述烟气换热器的第一换热通道的入口与与低热值气体燃烧器3的第二路气流通道36的出口连通。
进一步的改进实施例为：所述的冷凝除湿进一步的改进实施例为：所述的冷凝除湿器5与冷却塔的冷却水循环管路连接。
实施例3适用于含碳量较高的固体废物的高效炭化处理，通过管道从低热值燃烧器的燃烧室引出其中的一部分烟气进入燃烧热解器的炉排附近区域，由于引入的烟气温度极高(约850℃)但含氧量低，进入热解燃烧器后引起物料燃烧的比例较低，高温低氧空气直接接触物料具高效的加热效率可使其中的有机物快速热解气化。本实施例在运行过程中其炉排无需提供炉排底部的助燃风(可以沿用实施例1的基本设计但在使用时关闭助燃风机)，利用低氧高温烟气的热能替代物料燃烧的热能对物料进行热解，产出的渣料会保留较多的炭成分，渣料的资源化利用价值更高。
本发明适用于垃圾和污泥等固体废物的热解燃烧处理以及利用绿化垃圾和农产品秸秆等制炭。
以上所述仅为本发明的较佳实施例而已，并不用以限制本发明，凡在本发明的精神和原则之内所作的任何修改、等同替换和改进等，均应包含在本发明的保护范围之内。

Claims (9)

  1. 一种封闭式负压固体废物控氧热解装置，其特征是：包括烘干器、热解燃烧器、低热值气体燃烧器、烟气换热器、冷凝除湿器、热风循环风机、热解气抽风机和主风机，所述的烘干器设有物料进口、物料出口、热风进口和湿气排口，所述的热解燃烧器设有物料进口、出渣口和热解气出口，所述的低热值气体燃烧器设有进风口和烟气出口，所述的烟气换热器设有烟气进口、尾气出口、热风出口和循环回风口，烟气进口、尾气出口分别对应连通于所述烟气换热器的第一换热通道的进口、出口，热风出口和循环回风口分别对应连通于所述烟气换热器的第二换热通道的进口、出口；所述的烘干器的湿气排口、冷凝除湿器、烟气换热器的热风回口、烟气换热器的热风出口、热风循环风机、烘干器的热风进口依序通过热风循环管连接成闭式循环结构；所述的热解燃烧器的热解气出口通过热解气抽风机、热解气输送管和主风机与低热值气体燃烧器的进风口连接，所述的主风机进风口端的热解气输送管通过旁通管道连通热风循环管；所述的低热值气体燃烧器的烟气出口与烟气换热器的烟气进口连接；所述的烘干器的物料出口与热解燃烧器的物料入口之间通过物料提升机连接，物料提升机设于物料输送密封区内，烘干器的物料出口与热解燃烧器的物料入口之间通过物料输送密封区连通；所述的热解燃烧器其内的下方设有炉排，炉排下方从左到右设有多个助燃风室。
  2. 根据权利要求1所述的封闭式负压固体废物控氧热解装置，其特征是：所述的烘干器内设有连续输送带。
  3. 根据权利要求1所述的封闭式负压固体废物控氧热解装置，其特征是：炉排为单层炉排，炉排上方设有一层或多层输送物料链带。
  4. 根据权利要求1所述的封闭式负压固体废物控氧热解装置，其特征是：炉排是可连续热解和燃烧物料的炉排，炉排是往复式炉排。
  5. 根据权利要求1所述的封闭式负压固体废物控氧热解装置，其特征是：所述的热解燃烧器设有燃烧器。
  6. 根据权利要求1所述的封闭式负压固体废物控氧热解装置，其特征是：所述的热解燃烧器其内下方的助燃风室分别与第一助燃风机、第二助燃风机、第三助燃风机连通；
    所述的第二助燃风机其吸风口与冷凝除湿器入口前端的热风循环管连通；或第三助燃风机热解气输送管的分支管连通；第一助燃风 机与物料输送密封区内连通或与外界连通。
  7. 根据权利要求1所述的封闭式负压固体废物控氧热解装置，其特征是：所述的低热值气体燃烧器内设有用于第一路气流通道、第二路气流通道进行换热的换热区，以及燃烧室；第一路气流通道的入口连通低热值气体燃烧器的进风口，第一路气流通道的出口连通燃烧室，第二路气流通道的入口连通燃烧室，低热值气体燃烧器的进风口与第一路气流通道的入口连通。
  8. 根据权利要求7所述的封闭式负压固体废物控氧热解装置，其特征是：所述的烟气换热器为两路逆向气流换热的热交换器，所述烟气换热器的第一换热通道的入口与低热值气体燃烧器的第二路气流通道的出口连通。
  9. 根据权利要求1所述的封闭式负压固体废物控氧热解装置，其特征是：所述的低热值气体燃烧器其燃烧室与所述的热解燃烧器的炉排区域空间通过耐火隔热管道连通。
PCT/CN2021/111945 2021-03-15 2021-08-11 封闭式负压固体废物控氧热解装置 WO2022193537A1 (zh)

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