WO2022016801A1 - 一种生物质辐射微波耦合热解系统及方法 - Google Patents

一种生物质辐射微波耦合热解系统及方法 Download PDF

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WO2022016801A1
WO2022016801A1 PCT/CN2020/138200 CN2020138200W WO2022016801A1 WO 2022016801 A1 WO2022016801 A1 WO 2022016801A1 CN 2020138200 W CN2020138200 W CN 2020138200W WO 2022016801 A1 WO2022016801 A1 WO 2022016801A1
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pyrolysis
radiation
microwave
oil
gas
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French (fr)
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张会岩
李晓迪
张书平
肖睿
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Southeast University
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/28—Other processes
    • C10B47/32—Other processes in ovens with mechanical conveying means
    • C10B47/44—Other processes in ovens with mechanical conveying means with conveyor-screws
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/005—After-treatment of coke, e.g. calcination desulfurization
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/02—Multi-step carbonising or coking processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
    • C10B57/10—Drying
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Definitions

  • the invention relates to a pyrolysis system and method, in particular to a material radiation microwave coupled pyrolysis system and method.
  • Biomass mainly refers to lignocellulose such as straws and trees other than grains and fruits in the process of agricultural and forestry production, scraps of agricultural products processing industry, agricultural and forestry wastes, and livestock manure and waste in the process of animal husbandry production. It is the fourth largest energy source in the world. The utilization of biomass energy involves not only energy-related issues, but also environmental-related issues such as solid waste disposal.
  • Biomass pyrolysis refers to the process in which biomass is heated and heated in an anaerobic or hypoxic environment to cause internal decomposition to form biochar, bio-oil and pyrolysis gas. Pyrolysis is an important method for efficient utilization of biomass energy, but there are still many problems in the practical utilization of biomass pyrolysis, mainly including the following: traditional internal thermal pyrolysis furnace products have low output, poor quality, and low energy utilization efficiency ;External thermal pyrolysis furnace requires nitrogen or inert gas as carrier gas, the equipment is complex and the cost is high; Microwave pyrolysis has the advantages of no carrier gas, uniform heating, etc., but requires a large amount of electrical energy input to convert into microwave energy, while biomass raw materials microwave The absorption capacity is low, resulting in poor energy utilization; the biomass distribution is scattered, and the bulk density of the raw materials is low, and the transportation cost is high, making it difficult for large-scale centralized processing; the biomass raw materials generally have high moisture content, and the drying process consumes a lot of
  • the present invention aims to provide a biomass radiation microwave coupled pyrolysis system and method with no carrier gas and high energy utilization rate.
  • a biomass radiation microwave coupled pyrolysis system including a feeding system, an oil and gas separation system, and a radiation pyrolysis device and a microwave pyrolysis device arranged between the feeding system and the oil and gas separation system; the radiation
  • the inlet of the pyrolysis device is connected to the outlet of the feeding system.
  • the device is in the shape of a sleeve.
  • the outer layer circulates flue gas, and the inner layer conveys the feeding material.
  • the inner layer pyrolysis gas outlet and the radiation pyrolysis material outlet are respectively connected to the oil and gas separation system and the microwave pyrolysis system.
  • the device, the pyrolysis gas outlet and the microwave pyrolysis material outlet of the microwave pyrolysis device are respectively connected to the oil and gas separation system and the carbon condensation device.
  • the microwave pyrolysis device includes a microwave generator and a waveguide arranged at the central axis of the device. Equipped with a feeder port.
  • the biomass radiation microwave coupled pyrolysis method of the present invention comprises the following steps:
  • the material is fluidized and dried in a fluidized bed, and sent to a radiation pyrolysis device for low-temperature pyrolysis after cyclone separation;
  • the radiation pyrolysis device uses the heat of the flue gas generated by the combustion of the non-condensable gas after the oil and gas separation of the system for pyrolysis, and the pyrolysis temperature is 340 ° C ⁇ 360 ° C, and the product after the material pyrolysis is separated from oil and gas;
  • the material that has undergone radiation pyrolysis enters the microwave pyrolysis device for rapid pyrolysis, and the pyrolysis temperature is 600°C to 620°C, and the remaining solid material after pyrolysis is cooled.
  • the radiation low temperature pyrolysis of the present invention adopts high temperature flue gas to carry out radiation heat exchange on biomass, realizes pyrolysis without carrier gas, and can be directly connected with the microwave pyrolysis section, and the flue gas after heat exchange is further dried in the fluidized bed. materials to achieve gradient utilization of heat.
  • the energy consumption of low-temperature pyrolysis in the radiation pyrolysis section of the present invention accounts for more than 80% of the total energy consumption of biomass pyrolysis, and the microwave pyrolysis section only needs to input a small amount of electric energy to perform deep pyrolysis on biomass and obtain high-quality heat. After preheating and decomposing, the biomass absorption capacity is enhanced, the microwave energy consumption is reduced, the energy utilization efficiency is improved, and the high-quality oil and carbon co-production can be realized.
  • the present invention adopts the bubbling fluidization drying process in which biomass and gas are fully contacted, with high heat exchange efficiency and uniform heating;
  • the device of the present invention is small in size, can be arranged in a small space, can be used as a mobile device, and overcomes the limitation of biomass distribution and dispersion.
  • Fig. 1 is the structural representation of the system of the present invention
  • FIG. 2 is a schematic structural diagram of the microwave pyrolysis device of the present invention.
  • the system of the present invention includes a feeding system, an oil-gas separation system, a radiation pyrolysis device and a microwave pyrolysis system arranged between the feeding system and the oil-gas separation system.
  • the feeding system consists of a fluidized bed 2, a cyclone separator 3 located at the top outlet of the fluidized bed 2, a screw feeding device 1 located at the inlet of the fluidized bed, an air supply system 31 located at the bottom of the fluidized bed, and
  • the air lock 4 is arranged between the cyclone separator 3 and the radiation pyrolysis device 5 .
  • the radiation pyrolysis device 5 is a horizontally arranged casing structure, the outer layer is a high-temperature flue gas layer, and is provided with a flue gas inlet 8 and a flue gas outlet 30 .
  • the flue gas inlet 8 is connected to the burner 11, and the flue gas outlet 30 is connected to the air supply system 31 of the feeding system.
  • the inner layer is the material layer, and the inner layer is connected with the radiant pyrolysis gas outlet 6 .
  • the radiant pyrolysis gas outlet 6 is connected to the first heat exchanger of the oil-gas separation system.
  • the central axis of the radiation pyrolysis device 27 is provided with a spiral auger 7 driven by a motor, which is responsible for the conveying of materials.
  • the microwave pyrolysis device 27 is provided with a microwave pyrolysis gas outlet 19 and a microwave pyrolysis material outlet.
  • the material outlet of the microwave pyrolysis device 27 is connected to the carbon condensation device 23, and the microwave pyrolysis gas outlet 19 is connected to the second heat exchange of the oil-gas separation system. device.
  • the central axis of the radiation pyrolysis device 27 is also provided with a spiral auger driven by a motor, which is responsible for the conveying of materials. As shown in FIG.
  • a waveguide 25 is provided on the central axis of the radiation pyrolysis device 27, and a plurality of feed ports 26 are arranged on the waveguide 25.
  • the microwaves enter the radiation pyrolysis device from the feed ports through the waveguide. It can ensure the integrity of the resonant cavity in the microwave pyrolysis device, reduce the difficulty of sealing, and make the microwave radiation more uniform.
  • the charcoal condensation device 23 is in the shape of a casing, and the outer layer of the device circulates cooling water, and the outer layer is provided with a cooling water inlet and a cooling water outlet.
  • the central axis of the inner layer of the device is provided with a spiral auger driven by a motor, and the outlet of the device is connected to the carbon storage tank 22 .
  • the oil and gas separation system includes a primary oil and gas separation device 12, a first heat exchanger, a second heat exchanger, and a secondary oil and gas separation device 17.
  • the first heat exchanger and the second heat exchanger are respectively connected to the outlets of the radiation pyrolysis device and the microwave pyrolysis device.
  • the separation device 12 is connected in parallel with the secondary oil and gas separation device 17 .
  • a vacuum pump 15 is provided in front of the inlet of the secondary oil and gas separation device 17 , and the outlet of the secondary oil and gas separation device 17 is connected to a gas storage tank 14 for storing non-condensable gas.
  • Both the primary and secondary oil and gas separation devices include an oil storage tank arranged below the separation chamber, a non-condensable gas outlet and a pyrolysis gas inlet arranged above the separation chamber.
  • the gas storage tank 14 is connected to the burner 11, and the burner 11 is also provided with a blower.
  • the burner burns the stored non-condensable gas to generate high-temperature flue gas, which is passed into the outer layer of the radiation pyrolysis device 5 to provide radiation pyrolysis heat.
  • the fluidized bed 2 , the microwave pyrolysis device 5 and the radiation pyrolysis device 27 are all provided with thermal insulation layers.
  • biomass passes through screw feeding device 1 and enters fluidized bed 2 for drying. 250°C. After drying, the biomass is separated by the cyclone 3, and the discharge temperature is 110-130 °C. After passing through the air lock 4, it enters the radiation pyrolysis device 5 for low-temperature pyrolysis, and the pyrolysis temperature is 340-360 °C.
  • the biomass is transported by the motor-driven auger 7, and the vacuum pump 15 evacuates the lining of the device, so that the interior is in a vacuum state.
  • the pyrolysis gas phase product enters the primary oil and gas separation device 12 through the first heat exchanger through the pyrolysis gas outlet 6 of the radiation pyrolysis section for gas-liquid separation, and the tar enters the low temperature pyrolysis oil storage tank 10 .
  • the high-temperature flue gas that provides the heat source for radiation pyrolysis is produced by the combustion of non-condensable gas in the burner 1, and enters the outer layer of the radiation pyrolysis device 5 through the flue gas inlet 8.
  • the heat is mainly radiative heat exchange, and the temperature of the flue gas after heat exchange is 750-800 ° C. After mixing with the cold air through the flue gas outlet 30, it is sent to the drying device by the fluidized bed air supply system 31 for further use.
  • the biomass After the biomass undergoes low-temperature pyrolysis, it then enters the microwave pyrolysis device 27 for rapid pyrolysis.
  • the device is evacuated by the vacuum pump 15, and microwaves are generated by the microwave generator 20. Rapid pyrolysis is performed in the microwave pyrolysis device 27.
  • the temperature is 600-620°C, and the auger is driven by the motor 28 to push the biomass.
  • the pyrolysis solid product enters the charcoal cooling device 23 , the cooling water enters from the water inlet 21 , and is discharged from the water outlet 24 for countercurrent heat exchange, and the biomass pyrolysis product biochar is collected by the carbon storage tank 22 .
  • the pyrolysis gas product is sent to the first and second heat exchangers through the pyrolysis gas outlet 19 of the microwave pyrolysis section, separated by the first-stage oil and gas separation device 12, and the liquid phase enters the rapid pyrolysis oil storage tank 16.
  • the gas products of the latter radiation pyrolysis stage are combined, and continue to enter the secondary oil and gas separation device 17 through the vacuum pump 15 to complete the separation of non-condensable gas and light oil, and are respectively sent to the gas storage tank 14 and the light oil tank 18.
  • the non-condensable gas is sent into the burner 11 from the gas storage tank 14, and the air is sent into the air by the blower 13 to supply oxygen and adjust the air excess coefficient to control the temperature of the flue gas.
  • the fluidized bed 2 , the radiation pyrolysis device 5 and the microwave pyrolysis device are covered with an insulating layer 29 to reduce heat dissipation.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

一种生物质辐射微波耦合热解系统及方法，系统包括设于给料系统和油气分离系统之间的辐射热解装置(5)和微波热解系统；辐射热解装置(5)呈套管状，外层内部流通烟气，内层输送给料，辐射热解装置(5)出口分别连接油气分离系统和微波热解系统；微波热解系统包括微波热解装置(27)和炭冷凝装置(23)，微波热解装置(27)出口分别连接炭冷凝装置(23)和油气分离系统，该微波热解装置(27)包括微波发生器(20)以及设于其内部中轴线处的波导管(25)，波导管(25)上设有馈波口(26)。辐射热解采用高温烟气对生物质进行辐射换热，实现无载气热解，可直接与微波热解段相连，换热后的烟气进一步干燥流化床(2)内的物料，实现热量的梯度利用。

Description

一种生物质辐射微波耦合热解系统及方法 技术领域
本发明涉及一种热解系统及方法，尤其涉及一种物质辐射微波耦合热解系统及方法。
背景技术
生物质主要是指农林业生产过程中除粮食、果实以外的秸秆、树木等木质纤维素、农产品加工业下脚料、农林废弃物及畜牧业生产过程中的禽畜粪便和废弃物等物质，其是世界第四大能源。生物质能源化利用涉及的不仅是能源相关问题，其还涉及固体废弃物处置等环境相关问题。
生物质热解是指生物质在绝氧或低氧环境下加热升温引起内部分解形成生物炭、生物油和热解气的过程。热解是高效利用生物质能的重要方法，但生物质热解在实际利用中仍存在诸多问题，主要有以下几点：传统内热式热解炉产品产量低、品质差、能量利用效率较低；外热式热解炉需要氮气或惰性气体作载气，设备复杂且成本高；微波热解有无需载气、加热均匀等优点，但需要大量电能输入转化为微波能，同时生物质原料微波吸收能力较低，导致能量利用率较差；生物质分布分散，且原料堆积密度低，运输成本高，难以大规模集中化处理；生物质原料普遍含水率较高，干燥过程耗能较大。
发明内容
发明目的：本发明旨在提供一种无载气、能量利用率高的生物质辐射微波耦合热解系统及方法。
技术方案：一种生物质辐射微波耦合热解系统，包括给料系统、油气分离系统，还包括设于给料系统和油气分离系统之间的辐射热解装置和微波热解装置；所述辐射热解装置入口连接给料系统出口，该装置呈套管状，外层内部流通烟气，内层输送给料，内层热解气出口、辐射热解物料出口分别连接油气分离系统和微波热解装置，微波热解装置的热解气出口和微波热解物料出口分别连接油气分离系统和炭冷凝装置，微波热解装置包括微波发生器以及设于装置内部中轴线处的波导管，波导管上设有馈波口。
本发明所述的生物质辐射微波耦合热解方法，包括以下步骤：
(1)物料经过流化床流化干燥，并经过旋风分离后送入辐射热解装置进行低温热解；
(2)辐射热解装置利用系统油气分离后的不冷凝气体燃烧产生的烟气热量进行热解，热解温度340℃～360℃，物料热解后的产物再进行油气分离；
(3)经过辐射热解的物料进入微波热解装置进行快速热解，热解温度为600℃～620℃，热解后的剩余固体物料进行冷却。
有益效果：与现有技术相比，本发明具有如下显著优点：
(1)本发明辐射低温热解采用高温烟气对生物质进行辐射换热，实现无载气热解，可 直接与微波热解段相连，换热后的烟气进一步干燥流化床内的物料，实现热量的梯度利用。
(2)本发明辐射热解段低温热解耗能占生物质热解总耗能的80％以上，微波热解段只需输入少量电能即可对生物质进行深度热解，获得高品质热解产品，进行预热解后生物质吸波能力增强，减少微波耗能，提高能量利用效率，实现高品质油炭联产，同时控制设备尺寸，可作为移动式设备使用，适应生物质分散特点。
(3)本发明采用鼓泡流化干燥该过程生物质与气体充分接触，换热效率高，受热均匀；
(4)本发明装置尺寸较小，且能在较小空间内完成布置，可作为移动式装置进行使用，克服生物质分布分散的限制。
附图说明
图1为本发明系统的结构示意图；
图2为本发明微波热解装置的结构示意图。
具体实施方式
下面结合附图对本发明的技术方案作进一步说明。
如图1所示，本发明的系统包括给料系统、油气分离系统、设于给料系统和油气分离系统之间的辐射热解装置和微波热解系统。
给料系统由流化床2、设于流化床2顶部出口处的旋风分离器3、设于流化床入口处的螺旋进料装置1、设于流化床底部的送风系统31以及设于旋风分离器3和辐射热解装置5之间的锁气器4。
辐射热解装置5为水平设置的套管结构，外层为高温烟气层，设有烟气入口8和烟气出口30。烟气入口8连接燃烧器11，烟气出口30连接给料系统的送风系统31。内层是物料层，内层连接有辐射热解气出口6。辐射热解气出口6连接油气分离系统的第一换热器。辐射热解装27置内部的中轴线设有由电机驱动的螺旋状绞龙7，负责物料的输送。
辐射热解装置5一端设有辐射热解物料出口，出口连接微波热解装置27入口。微波热解装置27设有微波热解气出口19和物微波热解料出口，微波热解装置27的物料出口连接炭冷凝装置23，微波热解气出口19连接油气分离系统的第二换热器。辐射热解装置27内部的中轴线也设有由电机驱动的螺旋状绞龙，负责物料的输送。如图2所示，辐射热解装置27内部的中轴线设有波导管25，波导管25上设有若干馈波口26，微波经波导管由馈波口进入辐射热解装置，波导管置于中轴内可以保证微波热解装置内谐振腔的完整性，减小密封的难度，同时使微波辐射更加均匀。
炭冷凝装置23呈套管状，装置外层流通冷却水，外层设有冷却水入口和冷却水出口，冷却水入口设于物料出口一侧，使得冷却水与物料形成逆流，增加换热效果。装置内层中轴线处设有由电机驱动的螺旋状绞龙，装置出口连接储炭罐22。
油气分离系统包括一级油气分离装置12、第一换热器、第二换热器以及二级油气分离 装置17。第一换热器和第二换热器分别连接辐射热解装置和微波热解装置的出口，一级油气分离装置12设有两个，分别连接第一、第二换热器，一级油气分离装置12并联并连接二级油气分离装置17。二级油气分离17装置入口前设有真空泵15，二级油气分离装置17出口连接用于存储不冷凝气体的储气罐14。一、二级油气分离装置均包括设于分离室下方的储油罐、设于分离室上方的不冷凝气体出口以及热解气入口。
储气罐14连接燃烧器11，燃烧器11还设有送风机，燃烧器内燃烧存储的不冷凝气体，产生高温烟气，通入辐射热解装置5的外层中提供辐射热解热量。
流化床2、微波热解装置5和辐射热解装置27的外部均设有保温层。
本发明的系统的工作原理如下：
首先，生物质经过螺旋进料装置1，进入流化床2进行干燥，热源为由流化床送风系统31送入的辐射热解利用后烟气和冷空气的混合气体，温度为200～250℃。随后干燥后生物质经旋风分离器3分离，出料温度为110～130℃，经过锁气器4，进入辐射热解装置5进行低温热解，热解温度340-360℃。
其次，在辐射热解装置5内生物质由电机带动绞龙7完成输送，真空泵15对装置内衬进行抽气，使其内部呈真空状态。热解气相产物经辐射热解段热解气出口6经第一换热器进入一级油气分离装置12进行气液分离，焦油进入低温热解储油罐10。为辐射热解提供热源的高温烟气由不冷凝气体在燃烧器1燃烧产生，经烟气入口8进入辐射热解装置5的外层，温度为1000-1150℃，装置内层接近真空，换热以辐射换热为主，换热后的烟气温度为750-800℃，经烟气出口30与冷空气混合后由流化床送风系统31送入干燥装置继续利用。
生物质经过低温热解后，随后进入微波热解装置27进行快速热解，装置内由真空泵15抽真空，由微波发生器20产生微波，在微波热解装置27内进行快速热解，热解温度600-620℃，由电机28带动绞龙推动生物质。
热解固体产物进入炭冷却装置23，冷却水由进水口21进入，出水口24排出，进行逆流换热，生物质热解产物生物炭由储炭罐22收集。
最后，热解气体产物经微波热解段热解气出口19送入第一、二换热器，经一级油气分离装置12分离，液相进入快速热解储油罐16，气体与经冷凝后的辐射热解段气体产物汇合，继续经真空泵15进入二级油气分离装置17完成不冷凝气体与轻质油的分离，分别送入储气罐14和轻质油罐18。不冷凝气体由储气罐14送入燃烧器11，并由送风机13送入空气供氧并调节空气过量系数从而控制烟气温度。流化床2、辐射热解装置5以及微波热解装置均有保温层29覆盖，减少热量耗散。

Claims (10)

  1. 一种生物质辐射微波耦合热解系统，包括给料系统、油气分离系统，其特征在于，还包括设于给料系统和油气分离系统之间的辐射热解装置(5)和微波热解装置(27)；所述辐射热解装置(5)入口连接给料系统出口，该装置呈套管状，外层内部流通烟气，内层输送给料，内层热解气出口(6)、辐射热解物料出口分别连接油气分离系统和微波热解装置(27)，微波热解装置(27)的热解气出口(19)和微波热解物料出口分别连接油气分离系统和炭冷凝装置(23)，微波热解装置(27)包括微波发生器(20)以及设于装置内部中轴线处的波导管(25)，波导管上设有馈波口(26)。
  2. 根据权利要求1所述的生物质辐射微波耦合热解系统，其特征在于，所述辐射热解装置(5)外层上设有烟气入口(8)，烟气入口(8)连接燃烧器(11)，燃烧器(11)内燃烧油气分离系统分离得到的不冷凝气体。
  3. 根据权利要求1所述的生物质辐射微波耦合热解系统，其特征在于，所述炭冷凝装置(23)呈套管状，装置外层设有冷却水入口(21)和冷却水出口(24)，装置内层中轴线处设有由电机驱动的螺旋状绞龙，装置出口连接储炭罐(22)。
  4. 根据权利要求1所述的生物质辐射微波耦合热解系统，其特征在于，所述给料系统包括流化床(2)、设于流化床顶部出口处的旋风分离器(3)、设于流化床底部的送风系统(31)以及设于旋风分离器(3)和辐射热解装置(5)之间的锁气器(4)；所述流化床(2)设有给料入口，入口处设有螺旋进料装置(1)。
  5. 根据权利要求2或4所述的生物质辐射微波耦合热解系统，其特征在于，所述所述辐射热解装置(5)外层上设有烟气出口(30)，烟气出口连接送风系统(31)。
  6. 根据权利要求1所述的生物质辐射微波耦合热解系统，其特征在于，所述油气分离系统包括一级油气分离装置(9)、第一换热器、第二换热器以及设于一级油气分离装置后的真空泵(15)；所述第一换热器和第二换热器分别连接辐射热解物料出口和微波热解物料出口，一级油气分离装置(9)设有两个，分别连接第一、第二换热器。
  7. 根据权利要求6所述的生物质辐射微波耦合热解系统，其特征在于，所述油气分离系统还包括二级油气分离装置(17)，一级油气分离装置(9)并联并连接二级油气分离装置(17)；所述二级油气分离装置(17)出口连接储气罐(14)。
  8. 根据权利要求1所述的生物质辐射微波耦合热解系统，其特征在于，所述微波热解装置(27)和辐射热解装置(5)内部均设有由电机驱动的螺旋状绞龙。
  9. 根据权利要求1或4所述的生物质辐射微波耦合热解系统，其特征在于，所述流化床(2)、微波热解装置(27)和辐射热解装置(5)外部设有保温层。
  10. 一种生物质辐射微波耦合热解方法，基于权利要求1～9任一项所述的热解系统，其特征在于，包括以下步骤：
    (1)物料经过流化床流化干燥，并经过旋风分离后送入辐射热解装置进行低温热解；
    (2)辐射热解装置利用系统油气分离后的不冷凝气体燃烧产生的烟气热量进行热解，热解温度340℃～360℃，物料热解后的产物再进行油气分离；
    (3)经过辐射热解的物料进入微波热解装置进行快速热解，热解温度为600℃～620℃，热解后的剩余固体物料进行冷却。
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