WO2012129814A1 - 一种有机物热解制取活性炭方法 - Google Patents

一种有机物热解制取活性炭方法 Download PDF

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WO2012129814A1
WO2012129814A1 PCT/CN2011/072388 CN2011072388W WO2012129814A1 WO 2012129814 A1 WO2012129814 A1 WO 2012129814A1 CN 2011072388 W CN2011072388 W CN 2011072388W WO 2012129814 A1 WO2012129814 A1 WO 2012129814A1
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pyrolysis
combustible gas
reforming
gas
temperature
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PCT/CN2011/072388
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English (en)
French (fr)
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李爱民
高宁博
毛燎原
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大连理工大学
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Priority to US14/115,625 priority Critical patent/US9650254B2/en
Priority to PCT/CN2011/072388 priority patent/WO2012129814A1/zh
Publication of WO2012129814A1 publication Critical patent/WO2012129814A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/30—Active carbon
    • C01B32/312—Preparation
    • C01B32/318—Preparation characterised by the starting materials
    • C01B32/324—Preparation characterised by the starting materials from waste materials, e.g. tyres or spent sulfite pulp liquor
    • 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
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/08—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form
    • C10B49/10—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form according to the "fluidised bed" technique
    • 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
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/023—Reducing the tar content
    • 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
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the invention belongs to the field of organic matter pyrolysis and activated carbon technology, and relates to a method for preparing activated carbon by pyrolysis of organic matter.
  • it relates to the use of organic materials including organic solid waste, biomass, coal, municipal sludge, oil-based sludge, plastics, rubber, organic waste and its derivatives to prepare pyrolysis and activated carbon preparation methods.
  • Pyrolysis is an effective method for resource recycling of organic matter.
  • products such as combustible gas, tar, coke, and the like can be obtained.
  • the combustible gas and the tar contain a high calorific value, and the coke can be activated to form activated carbon.
  • Activated carbon is a product with high economic value and is widely used in various industrial processes and daily life.
  • the process of pyrolysis of organic matter requires a large amount of energy. At present, most of the pyrolysis process provides heat for pyrolysis by consuming external energy, and the process energy consumption is high.
  • the activation of coke is also caused by the addition of gases such as water vapor, CO 2 , air (mainly oxygen) or mixtures thereof as activation media. These activation methods consume additional energy to provide heat for the activation process.
  • the high temperature combustible gas generated in the pyrolysis process of organic matter and the heat value contained in the combustible gas can provide the heat required for the organic pyrolysis process.
  • the tar produced during the pyrolysis process is often entrapped in flammable gas, which is the source of problems such as blockage of pipes and corrosion of equipment.
  • the pyrolysis tar has a high calorific value, and the reforming of the pyrolysis combustible gas can improve the grade of the combustible gas and reduce the discharge of the tar.
  • Patent application number is 201010159906.X
  • the technical scheme named 'Method for low-temperature pyrolysis of municipal sludge simultaneously preparing bio-oil and activated carbon' refers to the low-temperature fluidization pyrolysis method of urban sludge, which requires a large amount of external energy to heat the reactor and pyrolyze the combustible gas.
  • the sensible heat in the medium cannot be fully utilized and cannot solve many problems caused by tar.
  • the invention aims at the problem that the organic matter pyrolysis process and the activated carbon preparation process consume high energy, and provides a combustible gas generated by the pyrolysis reaction of the organic substance as a pyrolysis process and an energy source.
  • the generated high temperature is heated by the heat storage heat exchange to heat the combustible gas, and the high-temperature combustible gas is used as a pyrolysis medium to carry out pyrolysis reaction of the organic matter.
  • the zero supply of external energy during the pyrolysis of organic matter is achieved, and the cheap production of pyrolysis activated carbon is realized.
  • the method for preparing activated carbon by pyrolysis of organic matter of the invention comprises organic matter pyrolysis process, reforming process, organic matter drying process, flammable gas purification process and heat storage combustion heat exchange process.
  • the organic matter is pyrolyzed as a pyrolysis feedstock in an organic pyrolysis apparatus to produce combustible gas, tar, and coke.
  • the combustible gas passes through the gas-solid separation device and the high-temperature dust removal device, and then enters the reforming device for partial combustion and heat storage reforming, and the tar component in the pyrolysis gas is decomposed.
  • the reforming device is a high-temperature reforming reaction device, and the reforming medium is a catalyst, and the tar component in the combustible gas is catalytically reformed by the reforming device. After the reforming, the tar component in the combustible gas is greatly reduced, and the calorific value of the combustible gas is increased after reforming.
  • the combustible gas coming out of the reforming device enters the drying device, and the combustible gas is cooled by the heat exchange heating device.
  • the wet material added from the inlet of the drying device is dried, and the organic matter produced after drying enters the pyrolysis device as a pyrolysis material to participate in the reaction.
  • the combustible gas enters the drying device after passing through the reforming device, and the drying process is used for recovering sensible heat in the combustible gas; after drying, the moisture content of the organic matter is greatly reduced.
  • the cooled combustible gas enters the gas storage device after passing through the purification device.
  • the combustible gas stored in the gas storage device is burned in the high-temperature regenerative combustion device, and the high-temperature flue gas generated by the combustion keeps the regenerative combustion device at a relatively high temperature level, and the discharged exhaust gas is discharged through the heat exchanger.
  • the combustible gas extracted from the gas storage device is divided into two parts, one part is burned as a fuel in the regenerative combustion device, and the other part is heated in the regenerative combustion device. A large amount of heat is generated during combustion to heat the combustible gas into a high-temperature combustible gas.
  • the regenerative combustion device has channels in two directions, one in the combustion channel and the other in the heat exchange channel.
  • the combustible gas is combusted from the gas storage device while the combustible gas is combusted, and the combustible gas is taken out through the heat exchange passage for heat exchange.
  • the combustible gas is rapidly heated to form a high-temperature combustible gas.
  • the blower connected to the regenerative combustion device generates cold air to recover the residual heat of the flue gas discharged from the regenerative combustion device through the air preheating device, thereby preheating the air, and the formed hot air is used for the combustion supply of the regenerative combustion device.
  • the high-temperature combustible gas from the regenerative combustion device enters the pyrolysis device as a pyrolysis medium to provide heat for the pyrolysis reaction, and also acts as an activator to activate the coke in the pyrolysis process to generate activated carbon.
  • the combustible gas component in the pyrolysis process may be H 2 , CO , CO 2 , CH 4 , C 2 H 4 , C 2 H 6 , C 3 H 6 , C 3 H 8
  • the inlet temperature of the pyrolysis medium may be For 600-800 o C
  • the organic matter entering the pyrolysis unit may have a water content of 20-30%
  • the reforming device may be a high temperature reforming reaction device, and the working temperature of the reforming device may be
  • the temperature of the regenerative combustion unit can be 800-900 o C; the preheating temperature of the regenerative combustion flue gas preheating recovery process is 150-200 o C.
  • the pyrolysis medium is a combustible gas, and the pyrolysis medium is both a heat carrier and an activator to activate the coke, thereby activating the coke into activated carbon.
  • the regenerative combustion process can realize the regenerative combustion of the combustible gas, and can clean and efficiently exchange the combustible gas.
  • the drying process can utilize the sensible heat in the combustible gas to achieve the drying of the organic matter, the energy is fully utilized and saved, and the organic matter is converted from the solid waste into the fuel, thereby improving the organic material position.
  • the reforming process reforms the tar component in the pyrolysis gas to reduce the tar component in the pyrolysis combustible gas and increase the calorific value of the combustible gas.
  • Figure 1 is a schematic view of the structure of a device according to the invention.
  • Figure 1 is a diagram showing the basic system arrangement of a processing apparatus for carrying out an organic matter pyrolysis process for producing activated carbon according to the present invention.
  • the organic matter is pyrolyzed as a pyrolysis feedstock in a pyrolysis reactor to produce a combustible gas and a fixed char.
  • the combustible gas enters the reforming device through the gas-solid separation device and the high-temperature dust removing device to perform a reforming reaction, and the tar component in the combustible gas is decomposed, and the calorific value of the combustible gas is improved.
  • the hot combustible gas from the reforming device passes through an organic drying device, and the wet organic matter completes the drying process by absorbing the sensible heat in the hot combustible gas, and the dried organic matter is input into the pyrolysis device as a pyrolysis raw material.
  • the high temperature regenerative combustion device has two channel directions, one is the direction of the combustion channel, and the other is the direction of the heat exchange channel.
  • the combustible gas passing through the drying device passes through the purifying device and enters the gas storage device; two gas conveying pipes are taken out from the gas storage device, one is connected with the combustion passage of the high-temperature regenerative combustion device, and the other is exchanged with the high-temperature regenerative combustion device. Hot channel direction connection.
  • the combustible gas is burned at a high temperature in the high-temperature regenerative combustion device, and the temperature of the regenerator is increased, and the generated flue gas is preheated by an air heat exchanger to preheat the cold air.
  • the air enters the combustion regenerator as an oxidant to participate in the combustion reaction; at the same time, in the direction of the other passage of the high-temperature regenerative combustion device, the combustible gas drawn from the gas storage device passes through the heat exchange direction passage of the high-temperature combustion device, and is low-temperature combustible. The gas is heated to a high-temperature combustible gas.
  • These high-temperature combustible gases enter the pyrolysis device as a pyrolysis medium to provide heat for the pyrolysis reaction, and also act as an activator to activate the coke in the pyrolysis process, thereby producing activated carbon.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
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Description

一种有机物热解制取活性炭方法
技术领域
本发明属于有机物热解及活性炭技术领域，涉及一种有机物的热解制取活性炭的方法。特别涉及到利用有机物包括有机固体废物、生物质、煤、城市污泥、油田含油污泥，塑料类、橡胶类、有机垃圾及其衍生物等有机物制取热解及活性炭制取方法。
背景技术
有机物种类繁多，产量巨大。热解是一种对有机物资源化处理的有效方法。通过热解有机物可得到可燃气体、焦油、焦炭等产物。可燃气体、焦油含有较高热值，焦炭经活化后可形成活性炭。活性炭是一种经济价值较高的产品，广泛用于各类工业过程及日常生活中。
热解有机物的过程需要消耗大量的能源。目前大多热解过程以消耗外来能源为热解提供热量，过程能耗较高。对焦炭的活化也多以外来气体如水蒸汽、 CO2 、空气（主要是氧）或它们的混合物为活化介质，这些活化方法多要消耗额外的能源来提供活化过程的热量。
有机物热解过程中产生的高温可燃气和可燃气体中蕴含的热值可以为有机物热解过程提供所需的热量。充分利用可燃气体中的显热和燃气热值，可以大大节约外来能量的供给。热解过程中产生的焦油往往裹挟在可燃气中，成为管道堵塞、设备腐蚀等问题的根源。热解焦油具有较高的热值，对热解可燃气体的重整，可以提升可燃气的品位，降低焦油的排放。
经检索发现了专利申请号为 200810123383.6 、名称为'城市污泥与农业废弃物共热解制备活性炭工艺 '的技术方案。该方案中提到了城市污泥与农业废弃物共热解制备活性炭工艺，这种方式将混合物在一定温度下隔绝空气加热，该方法需要外来能源对热解过程加热，能耗较高，物料密闭于反应器中，物料的流化性差。专利申请号为 201010159906.X 、名称为'城市污泥低温热解同时制备生物油和活性炭的方法'的技术方案，提到了城市污泥低温流化热解方法，该方法需要大量的外来能源加热反应器，热解可燃气体中的显热不能得到充分利用，不能解决焦油带来的诸多问题。
发明内容
本发明针对有机物热解过程以及活性炭制备过程中需要消耗较高的能量的问题，提供一种利用有机物通过热解反应产生的可燃气体为热解过程和提供能源。通过重整和净化后的可燃气体，经过高温蓄热重整装置后，产生的高温经蓄热换热后对可燃气体加热，以高温可燃气体为热解介质，进行有机物的热解反应。达到有机物热解过程中外来能量的零供给，实现热解活性炭的廉价生产。
本发明的有机物热解制取活性炭方法，包括有机物热解过程、重整过程、有机物干燥过程、可燃气体的净化过程和蓄热燃烧换热过程。
热解过程中，有机物作为热解原料在有机物热解装置内进行热解，产生可燃气体、焦油和焦炭。热解后可燃气体经过气固分离装置、高温除尘装置后，进入重整装置中进行部分燃烧蓄热重整，热解气中的焦油成分被分解。重整装置为高温重整反应装置，重整介质为催化剂，对可燃气体中的焦油成分经过重整装置进行催化重整。重整后可燃气体中的焦油组分大幅减低，可燃气体热值经重整后提高。
从重整装置出来的可燃气体进入干燥装置，通过换热加热干燥装置，可燃气体被冷却。从干燥装置入口处加入的湿物料被干燥，干燥后产生的有机物作为热解原料进入热解装置中参与反应。干燥过程中，可燃气体经重整装置后进入干燥装置，干燥过程用于回收可燃气体中的显热；经过干燥后，有机物的含水率大大降低。
冷却后的可燃气体经过净化装置后进入储气装置。储气装置中储存的可燃气体在高温蓄热燃烧装置进行燃烧，燃烧产生的高温烟气使蓄热燃烧装置一直保持较高温度水平，排出的尾气经过换热器后排出。
从储气装置中引出的可燃气体分为两部分，一部分作为燃料在蓄热燃烧装置中燃烧，另一部分在蓄热燃烧装置中被加热。燃烧时产生大量的热量将可燃气体加热成高温可燃气体。
在蓄热燃烧装置中，蓄热燃烧装置有两个方向的通道，一个方向是燃烧通道，另外一个方向是换热通道。可燃气体在燃烧通道燃烧的同时，从储气装置引出可燃气体通过换热通道进行换热，在这个过程中可燃气体被快速加热，形成高温可燃气体。与蓄热燃烧装置相连的鼓风机产生冷空气通过空气预热装置回收蓄热燃烧装置排出的烟气余热，从而实现对空气的预热，形成的热空气用于蓄热燃烧装置的燃烧供给。
从蓄热燃烧装置出来的高温可燃气体作为热解介质进入热解装置为热解反应提供热量，同时也作为活化剂对热解过程中的焦炭进行活化，从而生成活性炭。
所述的有机物热解装置为流化床、沸腾床、循环流化床或固定床。
本发明，热解过程中可燃气体组分可以为 H2 、 CO 、 CO2 、 CH4 、 C2H4 、 C2H6 、 C3H6 、 C3H8 ，热解介质进口温度可以为 600-800oC ，进入热解装置中的有机物含水率可以为 20-30% ；
所述的重整装置可以为高温重整反应装置， 重整装置的工作温度可以为
800-900oC ；蓄热燃烧装置的工作温度可以为 800-900 oC ；蓄热燃烧烟气尾气预热回收过程中对空气的预热温度为 150-200oC 。
本发明的有益效果：
（ 1 ）有机物的热解与活性碳制备过程可充分利用有机物中蕴含的热值，实现外来能源的零供给，甚至可以对外提供能源。
（ 2 ）热解介质为可燃气体，热解介质既为热载体，又作为活化剂活化焦炭，从而使焦炭活化为活性炭。
（ 3 ）蓄热燃烧过程可以实现可燃气体的蓄热燃烧，可以对可燃气体进行清洁高效的换热。
（ 4 ）干燥过程可以利用可燃气体中的显热，实现有机物的干燥，能量得到充分利用和节约，将有机物从固体废物转化为燃料，提升了有机物品位。
（ 5 ）节约能源，整个***不需要其他外来能源。
（ 6 ）有效解决了气化燃气的净化问题。重整过程对热解气中的焦油成分进行重整，可降低热解可燃气体中的焦油成分，同时提升可燃气体热值。
附图说明
图 1 是根据本发明装置的结构示意图。
具体实施方式
下面结合附图对本发明的技术方案做进一步的说明。
图 1 所示是根据本发明用于实施有机物热解制取活性炭方法的处理装置的基本***布置。如图 1 所示，有机物作为热解原料在热解反应装置内进行热解，产生可燃气体和固定炭。可燃气体经过气固分离装置和高温除尘装置后进入重整装置中进行重整反应，可燃气体中的焦油成分被分解，可燃气体热值得到提高。从重整装置出来的热可燃气体经过一个有机物干燥装置，湿有机物通过吸收热可燃气体中的显热完成干燥过程，干燥后的有机物作为热解原料输入热解装置。高温蓄热燃烧装置有两个通道方向，一个是燃烧通道方向，一个是换热通道方向。通过干燥装置后的可燃气体经净化装置后进入储气装置；从储气装置引出两条输气管路，一条与高温蓄热燃烧装置的燃烧通道方向连接，另外一条与高温蓄热燃烧装置的换热通道方向连接。在高温蓄热燃烧装置的燃烧通道方向，可燃气体在高温蓄热燃烧装置内进行高温燃烧，蓄热体温度升高，产生的烟气通过一个空气换热器对冷空气进行预热，预热后的空气进入燃烧蓄热器作为氧化剂参与燃烧反应；于此同时，在高温蓄热燃烧装置的另一个通道方向，从储气装置引出的可燃气体经过高温燃烧装置的换热方向通道，低温可燃气体被加热为高温可燃气体，这些高温可燃气体作为热解介质进入热解装置为热解反应提供热量，同时也作为活化剂对热解过程中的焦炭进行活化，焦炭从而生成活性炭。

Claims (1)

1、一种有机物热解制取活性炭方法， 包括有机物热解过程、重整过程、有机物干燥过程、可燃气体的净化过程和蓄热燃烧换热过程，其特征在于以下步骤，
热解过程中，有机物作为热解原料在有机物热解装置内进行热解，产生可燃气体、焦油和焦炭；热解后可燃气体经过气固分离装置、高温除尘装置后，进入重整装置中进行部分燃烧蓄热重整，热解气中的焦油成分被分解；重整装置为高温重整反应装置，重整介质为催化剂，对可燃气体中的焦油成分经过重整装置进行催化重整；
从重整装置出来的可燃气体进入干燥装置，通过换热加热干燥装置，可燃气体被冷却；从干燥装置入口处加入的湿物料被干燥，干燥后产生的有机物作为热解原料进入热解装置中参与反应；干燥过程中，可燃气体经重整装置后进入干燥装置，干燥过程用于回收可燃气体中的显热；
冷却后的可燃气体经过净化装置后进入储气装置；储气装置中储存的可燃气体在高温蓄热燃烧装置进行燃烧，燃烧产生的高温烟气使蓄热燃烧装置一直保持较高温度水平，排出的尾气经过换热器后排出；
从储气装置中引出的可燃气体分为两部分，一部分作为燃料在蓄热燃烧装置中燃烧，另一部分在蓄热燃烧装置中被加热；燃烧时产生大量的热量将可燃气体加热成高温可燃气体；
从蓄热燃烧装置出来的高温可燃气体作为热解介质进入热解装置为热解反应提供热量，同时也作为活化剂对热解过程中的焦炭进行活化，从而生成活性炭。
2 、根据权利要求 1 所述的方法，其特征在于： 所述的有机物热解装置为流化床、沸腾床、循环流化床或固定床。
3 、根据权利要求 1 所述的方法，其特征在于：所述的重整装置为高温重整反应装置。
4 、根据权利要求 1 所述的方法，其特征在于： 进入干燥装置的湿物料含水率为 60-80% 。
5 、根据权利要求 1 所述的方法，其特征在于： 重整装置的工作温度为800-900oC 。
6 、根据权利要求 1 所述的方法，其特征在于： 蓄热燃烧烟气尾气预热回收过程中对空气的预热温度为 150-200oC 。
7 、根据权利要求 3 所述的方法，其特征在于： 蓄热燃烧装置的工作温度为800-900 oC 。
PCT/CN2011/072388 2011-04-01 2011-04-01 一种有机物热解制取活性炭方法 WO2012129814A1 (zh)

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