WO2011103768A1 - 农作物秸秆制炭方法及装置 - Google Patents

农作物秸秆制炭方法及装置 Download PDF

Info

Publication number
WO2011103768A1
WO2011103768A1 PCT/CN2011/000265 CN2011000265W WO2011103768A1 WO 2011103768 A1 WO2011103768 A1 WO 2011103768A1 CN 2011000265 W CN2011000265 W CN 2011000265W WO 2011103768 A1 WO2011103768 A1 WO 2011103768A1
Authority
WO
WIPO (PCT)
Prior art keywords
tank
pyrolysis
oxygen supply
carbonization
straw
Prior art date
Application number
PCT/CN2011/000265
Other languages
English (en)
French (fr)
Inventor
王晓光
景静勇
张树勤
Original Assignee
山西工霄商社有限公司
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 山西工霄商社有限公司 filed Critical 山西工霄商社有限公司
Priority to BR112012021187A priority Critical patent/BR112012021187A2/pt
Priority to US13/579,147 priority patent/US9321966B2/en
Priority to EP11746810.8A priority patent/EP2540803B1/en
Priority to RU2012133192/05A priority patent/RU2573014C2/ru
Publication of WO2011103768A1 publication Critical patent/WO2011103768A1/zh
Priority to ZA2012/05861A priority patent/ZA201205861B/en
Priority to US15/136,514 priority patent/US10273412B2/en

Links

Classifications

    • 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
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/05—Preparation or purification of carbon not covered by groups C01B32/15, C01B32/20, C01B32/25, C01B32/30
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05D—INORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C; FERTILISERS PRODUCING CARBON DIOXIDE
    • C05D9/00—Other inorganic fertilisers
    • 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
    • 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
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/40—Solid fuels essentially based on materials of non-mineral origin
    • C10L5/44—Solid fuels essentially based on materials of non-mineral origin on vegetable substances
    • C10L5/447—Carbonized vegetable substances, e.g. charcoal, or produced by hydrothermal carbonization of biomass
    • 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
    • C10B1/00—Retorts
    • C10B1/02—Stationary retorts
    • C10B1/04—Vertical retorts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2200/00—Components of fuel compositions
    • C10L2200/04—Organic compounds
    • C10L2200/0461—Fractions defined by their origin
    • C10L2200/0469—Renewables or materials of biological origin
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/02—Combustion or pyrolysis
    • 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
    • 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
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the invention belongs to the technical field of straw pyrolysis carbonization, and in particular relates to a carbon method and device for crop straw.
  • the carbonization of crop straw plays an important role in the comprehensive utilization of straw.
  • the straw carbonization method and equipment have become more and more mature in the process of continuous technological improvement, but there are inevitably some defects.
  • the patent number is ZL200510044136.3, which is named as "the high temperature floating oxygen carbonization process of grass wood".
  • the required equipment is two inner and outer furnace bodies.
  • the furnace mouth is open, the carbonization starts, and the grass door has the furnace door mouth and is sent into the inner furnace. After deflagration, it decomposes rapidly, and the high-temperature gas is precipitated.
  • the rising and the floating oxygen in the air are fully contacted into a flame, the furnace mouth is sealed, the vegetation is continuously fed, and the carbonization is continued, and the carbonization is rapidly cooled down to the point of ignition.
  • Patent No. ZL01132888.6 entitled “Device for carbonized crop by-products, etc.” the device is formed by forming a bottom hole at the bottom of the can-shaped container with a lid at the top and vertically penetrating the heat flow tube in the bottom hole. At this time, the upper end of the heat flow tube is stopped at a position 10 cm from the top of the container, and the lower end protrudes 3 cm below the bottom of the container, and a lateral hole is formed in the side of the container to set the smoke tube connected thereto.
  • the container is protruded to the outside, and a skirt base supporting the entire container is provided at the lower end, and a part of the opening is used as an incineration port, and a heat insulating layer is provided on the side portion and the top portion of the container or the cover.
  • the charcoal charred by the device needs to be placed after fire extinguishing for about one night and then opened again, before proceeding to the next carbonization process.
  • the production of straw charcoal is limited, and the device is a fixed structure.
  • the transportation cost of crop by-products is extremely high, and it cannot meet the requirements of high efficiency, low cost and large-scale production.
  • the object of the present invention is to solve the defects of low pyrolysis carbonization efficiency, high cost of straw charcoal and limited production scale in the prior art, and to provide a crop straw for adapting to the needs of pyrolysis and carbonization of different types of crop straws. Carbon making method and device.
  • the present invention provides a carbon method for crop straw, which comprises a pyrolysis and a carbonization process, wherein the pyrolysis process is controlled by adjusting the oxygen supply in the pyrolysis process, and the pyrolysis and carbonization are respectively performed in separate pyrolysis cells. And in the carbonization tank, the straw is subjected to a pyrolysis process in the pyrolysis tank and then enters the carbonization tank for carbonization.
  • the straw carbon making method of the invention separates the pyrolysis carbonization process of the straw, and separately completes the pyrolysis and carbonization process of the straw in different equipment units to improve the productivity, and at the same time, through the controllable oxygen supply in the pyrolysis process.
  • the straw is rapidly increased in the pyrolysis tank to complete the drying and preheating process, so that the straw is rapidly pyrolyzed.
  • the invention also provides a combined crop straw charcoal device, comprising a pyrolysis tank, a carbonization tank and a controllable oxygen supply pipeline, wherein an oxygen supply pipeline control butterfly valve is arranged at an oxygen inlet of the oxygen supply pipeline,
  • the sub-oxygen supply port connected to the controllable oxygen supply pipe is connected to the pyrolysis tank, and the pyrolysis tank and the carbonization tank are two independent equipment units, and the pyrolysis tank is provided with one or more layers of plate-type furnaces inside, and carbonization
  • the pool is located below the discharge port of the pyrolysis tank, and the carbonization tank has a cover for the one-way aeration device.
  • the device separately performs the pyrolysis and carbonization processes of the straw in the independent equipment units, thereby improving the pyrolysis and carbonization efficiency.
  • the crop straw is sent to the pyrolysis tank, the straw is ignited by the combustible characteristics of the straw, and the straw is dried, preheated and partially pyrolyzed by the heat generated by the spontaneous combustion of the straw.
  • control the degree of opening and closing of the oxygen supply pipeline in order to achieve rapid temperature rise and effectively dry, preheat the straw, and control part of the heat
  • the degree of solution ensures that the straw is not excessively pyrolyzed into ash; after that, the straw is turned into the lower part of the pyrolysis tank, and the straw under the oxygen supply port in the pyrolysis tank is further pyrolyzed under anoxic state.
  • the combustible gas such as CO, H 2 , C n H m produced by the pyrolysis carbonization process enters the pyrolysis tank and is sub-combusted in the space above the oxygen supply port to increase the temperature of the pyrolysis tank, and the straw is in the end of the pyrolysis tank.
  • the straw is sent to the carbonization tank through the discharge port, and the cover with the one-way aeration device is sealed with oxygen, and different carbonization time in the carbonization tank is determined according to the use of the straw carbon.
  • the invention further comprises a flue gas collecting cover disposed above the pyrolysis tank, wherein the flue gas collecting cover communicates with the settling chamber through the flue, wherein the settling chamber is provided with one or more stages of partitions, and the top of one end of the settling chamber is connected with the flue, and the settling The other end of the chamber has an exhaust port at the top, and the lower end of the exhaust port is connected with an oil collecting cover, and an oil collecting barrel is arranged below the oil collecting cover.
  • the flue gas during the pyrolysis and carbonization of the crop straw enters the end of the settling chamber through the flue gas collecting hood and the flue, and then enters the other end from below the partition, and finally exits from the exhaust port at the top of the end of the settling chamber, through which the path is made.
  • the stroke of the flue gas is increased, the flow rate is slowed down, and the flue gas temperature is also lowered, and the suspended particulate matter in the flue gas settles at the bottom of the settling chamber.
  • the oil collecting cover is installed at the lower end of the exhaust port at the end of the settling chamber, the flue gas is discharged into the atmosphere through the sleeve liquid collecting cover, and the flue gas entering the settling chamber is naturally condensed, and the wood tar and the straw vinegar contained therein are collected by the oil.
  • the cover is adsorbed.
  • the invention has the following characteristics: (1) In the pyrolysis process, according to the difference of the straw type and the difference of the moisture content of the straw, the oxygen supply is controlled, and the straw is efficiently dried, preheated and heated in the pyrolysis tank. solution. (2) Separating the pyrolysis and carbonization processes of crop straws, which are completed by different equipment units, greatly improving the efficiency of pyrolysis and carbonization. (3) The combined structure design makes the straw pyrolysis carbonization equipment easy to transport to the straw production area, and is quickly assembled and produced, which solves the problem that the straw pyrolysis carbonization device cannot be transported and moved. (4) It is convenient for splitting and transshipment.
  • the straw pyrolysis carbonization equipment will be split and transported to a reasonable working area in time to reduce the high freight cost caused by straw transportation.
  • the equipment unit will be Rapid assembly through the bottom plate, brackets, and fasteners.
  • the equipment is split into basic basics and transported to another working place for assembly and straw charring.
  • Straw pyrolysis process The flue gas deposition chamber is adopted, and the suspended particulate matter in the flue gas flow settles to the bottom of the sedimentation chamber through the device in the sedimentation chamber, and the wood tar and the straw vinegar solution are naturally condensed and attached to the oil collection cover, and flow into the oil collection tank. Collected, the exhaust gas is harmlessly discharged into the atmosphere, ensuring environmental protection and pollution-free production process.
  • the straw charcoal produced by the invention is widely used for processing and producing solid fuel for rural residents to replace fossil fuel; for soil improvement, improving soil water content, gas permeability, increasing soil organic matter content, increasing crop yield, reducing crops The occurrence of pests and diseases; Pretreatment of raw straw for biogas production, reducing the volume of straw, facilitating transportation and storage, making biogas production more economical and safe.
  • Figure 1 is a schematic view of the structure of the present invention.
  • Figure 2 is a schematic view of the structure of the pyrolysis cell.
  • Figure 3 is a plan view of Figure 2.
  • the invention relates to a combined crop straw carbon making method, wherein the pyrolysis process is controlled by adjusting oxygen supply in the pyrolysis process, and pyrolysis and carbonization are carried out in separate pyrolysis tank 1 and carbonization tank 2, respectively. After the pyrolysis process is completed in the pyrolysis cell 1, it is then introduced into the carbonization cell 2 for carbonization.
  • a combined crop straw carbon-making device comprises a pyrolysis tank 1, a carbonization tank 2 and a controllable oxygen supply pipeline 3, and an oxygen supply port 4 of the oxygen supply pipeline 3 is provided.
  • the pyrolysis cell 1 is mounted on a support 19, the carbonization tank 2 is located on the lower lifting plate 20 at the lower portion of the pyrolysis cell 1, the tray 20 is placed on the rail 21, and the furnace 7 is fixed to the wall of the pyrolysis cell 1 by a shaft.
  • the oxygen supply pipe butterfly valve 5 is used for controlling the opening and closing of the oxygen inlet port 4, and the controllable oxygen supply pipe 3 is disposed below the furnace 7 of the pyrolysis tank 1 along the outer wall of the pyrolysis tank 1 and communicates with the exterior of the pyrolysis tank 1, the carbonization tank 2 with a one-way venting device cover, when the pressure is too large, the cover is jacked up to release gas.
  • One pyrolysis tank 1 can be correspondingly provided with one or more carbonization tanks 2.
  • the carbonization tank 2 can also be used for switching to carbonization products, which can ensure the continuous pyrolysis process.
  • a sub-oxygen supply port 6 communicating with the interior of the pyrolysis cell 1 is distributed on the controllable oxygen supply pipe 3, and the hot gas rises due to the combustion of the straw in the pyrolysis cell 1 to cause a difference in air pressure inside and outside the pyrolysis cell 1.
  • the butterfly valve 5 outside the heat-dissipating cell 1 is opened, the air outside the pyrolysis cell 1 enters the pyrolysis cell 1 through the oxygen supply pipe 3 due to the negative pressure to achieve the combustion-supporting effect.
  • the oxygen inlet 4 is completely opened to rapidly increase the temperature in the pyrolysis tank, so that the straw is quickly dried and preheated.
  • the temperature reaches 200-850 ° C, the degree of opening of the oxygen inlet 4 is gradually reduced, and oxygen is reduced into the pyrolysis tank 1 to avoid excessive pyrolysis of the straw to ash.
  • the present invention further includes a flue gas collecting cover 9 disposed above the pyrolysis cell 1, the flue gas collecting cover being placed in the upper portion of the pyrolysis cell 1 through the bracket 19, and the flue gas collecting cover 9 communicating with the sedimentation chamber 11 through the flue 10, the sedimentation chamber 11 is provided with one or more stages of partitions 12, the top of one end of the settling chamber 11 is connected with the flue 10, the top of the other end of the settling chamber 11 is provided with an exhaust port 13, and the lower end of the exhaust port 13 is connected with the oil collecting cover 14, the oil An oil collecting bucket 15 is provided below the collecting cover 14.
  • the oil collecting cover 15 has a tapered cylindrical shape with through holes on its surface.
  • the partition 12 has only one end connected to the settling chamber wall 11 and the other end separated from the wall of the settling chamber 11, such as the upper end of the first stage partition connected to the top of the settling chamber, the second stage partition connected to the bottom of the settling chamber, and so on.
  • a flue gas passage is formed in the settling chamber 11.
  • the sub-oxygen supply port 6 is disposed as one or more layers corresponding to the flap type furnace 7, and is independently controlled in layers, and the position of the sub-supply port 6 is lower than or flush with the corresponding flap type furnace 7 In the plane, the straw on each layer of furnace 7 can get enough oxygen.
  • the flap type furnace 7 is fixed on the hollow shaft 16, the hollow shaft 16 is in communication with the oxygen supply conduit 3, and the hollow shaft 16 is provided with a hollow shaft divided oxygen supply port. 17, the hollow shaft on the furnace is also the oxygen supply site.
  • the invention consists of four main equipment units, a pyrolysis tank 1, a carbonization tank 2, a flue gas collecting cover 9 and a settling chamber 11, and other auxiliary device components.
  • the dry and flammable crop straw is fed to the flap furnace 7 in the pyrolysis tank 1 and ignited.
  • the oxygen supply is in the process of rising hot gas of the straw burning, and the oxygen is automatically supplied to the pyrolysis tank 1 through the oxygen supply pipe 3 due to the generation of the negative pressure, thereby rapidly increasing the temperature in the thermal pyrolysis tank 1, so that the straw is quickly dried and preheated. And partially pyrolysis.
  • the flap furnace 7 is turned, so that all the straw on the furnace 7 falls into the lower part of the pyrolysis tank 1, in the process, a very small amount of combustion
  • the straw falls into the fire stage 18, so that the straw which is subsequently sent to the pyrolysis tank 1 is quickly ignited; and most of the straw falling into the lower part of the pyrolysis tank 1 continues to heat up to the pyrolysis temperature under the high temperature oxygen barrier state, this process avoids A part of the slender component of the straw is burned to ash at a high temperature due to an excessive supply of oxygen.
  • the main components of the straw are formed: all of the cellulose, hemicellulose and part of the lignin are pyrolyzed at this stage.
  • the straw enters the carbonization tank 2 through the discharge port 8 of the pyrolysis tank, and is immediately covered with a lid with a one-way aeration device to seal the oxygen, and the charcoal is continuously heated by the straw, according to the straw charcoal.
  • the carbonization time of the straw in the carbonization tank 2 is finally determined.
  • the flue gas in the pyrolysis process enters the settling chamber 11 through the flue gas collecting cover 9 and the flue, and the partitioning chamber 12 is disposed in the sedimentation chamber 11 in the longitudinal direction of the flue gas flow to separate the sedimentation chamber, which can effectively reduce the flue gas flow rate and reduce the flue gas.
  • the temperature and the suspended particulate matter in part of the flue gas are settled at the bottom of the settling chamber 11 and collected and collected.
  • the wood tar and the straw vinegar which are present in the flue gas during the pyrolysis and carbonization of the crop straw are naturally condensed by the sedimentation chamber and then adhered to the oil collection cover 14 and flow into the oil collection tank 15, and are collected and collected separately for disposal.
  • the exhaust gas is discharged into the atmosphere harmlessly through the exhaust port.

Description

农作物秸秆制炭方法及装置
技术领域
本发明属于秸秆热解炭化技术领域， 具体是一种农作物秸秆制炭方法 及装置。
背景技术
农作物秸秆炭化在秸秆综合利用中占有重要地位， 秸秆炭化方法及设 备已经在不断的技术改进过程中变得越来越成熟， 但也不可避免地存在一 些缺陷。
如专利号为 ZL200510044136.3名称为 "草木高温浮氧炭化工艺"的发 明， 其所需设备为内外两个炉体， 炉口是敞开的， 炭化开始， 草木有炉门 炉口送入内炉， 引燃后迅速分解， 析出高温燃气， 上升和空气中浮氧充分 接触化为火焰， 封住炉口， 草木连续送入， 连续炭化， 至炭化结束迅速降 温到着火点以下。 但是， 使用上述草木炭化工艺， 因投入内炉的草木由于 火焰封住内炉炉口使空气无法进入内炉下部， 使后续投入内炉的草木极易 产生炭化不足的情况， 同时炭化过程结束后， 炭从内炉中卸料过程繁琐， 与热解炭化时间相比， 卸料等辅助时间长， 操作人员的劳动强度大， 必须 等到投入内炉的草木全部炭化并在长时间降温后才能卸料， 卸料后再重新 开始投料、 炭化、 卸料的过程， 使生产不能连续进行， 浪费了大量时间， 生产效率极低， 同时设备为固定式结构， 草木秸秆的运输成本极高， 无法 满足高效率、 低成本、 规模化生产的要求；
专利号为 ZL01132888.6名称为 "炭化农作物的副产物等的装置"的发 明专利， 其装置是在顶部设置盖子的筒罐状容器的底部形成底孔并在该底 孔内垂直贯通热流筒， 这时， 该热流筒的上端止于离该容器的顶部 10cm的 位置， 同时， 下端向该容器的底部下方突出 3cm， 再在该容器的侧部形成 横孔， 使与其连通的烟流筒设置在该容器上并向侧外方突出， 在下端设置 支持该容器全体的裙状基座并将其一部分开口作为焚烧口， 再在该容器的 侧部及顶部乃至盖子上设置隔热层。 通过该装置炭化后的炭化物， 需要在 灭火后， 放置约一昼夜后再开盖取出， 之后才能继续下一次炭化过程， 使 秸秆炭产量受到了限制， 同时该装置为固定结构， 农作物副产物运输成本 极高， 也无法满足高效率、 低成本、 规模化生产的要求。
如使用传统土窑进行农作物秸秆炭化， 虽然一次性的产量大， 但生产 周期时间长达几天至十几天， 效率极低、 安全性差、 经济效益不佳， 而且 无法解决可悬浮颗粒物排放及木焦油、 秸秆醋液的收集造成环保性能差， 因而不具备推广价值。
发明内容
本发明的目的是解决现有技术中存在的热解炭化效率低， 秸秆炭成本 高、 规模化生产程度受限的缺点， 为适应热解炭化不同类型的农作物秸秆 的需要， 提供一种农作物秸秆制炭方法及装置。
为实现上述目的， 本发明提供的一种农作物秸秆制炭方法， 包括热解 和炭化过程， 热解过程中采用调节氧气供给的方式控制热解过程， 热解和 炭化分别在独立的热解池和炭化池中进行， 秸秆在热解池中完成热解过程 后再进入炭化池进行炭化。
本发明所述的秸秆制炭方法是将秸秆热解炭化过程分开， 在不同设备 单元中分别完成秸秆的热解和炭化过程， 以提高生产率， 同时在热解过程 中， 通过可控制的供氧方式， 使秸秆在热解池内迅速提高温度， 完成干燥、 预热过程， 使秸秆迅速热解。
为实现发明目的， 本发明还提供一种组合式农作物秸秆制炭装置， 包 括热解池、 炭化池和可控式供氧管道， 供氧管道的进氧口处设有供氧管道 控制蝶阀， 连接于可控式供氧管道上的分供氧口与热解池相通， 热解池和 炭化池为两个独立的设备单元， 热解池内部设有一层或多层翻板式炉箅， 炭化池设于热解池出料口的下方， 炭化池带有单向通气装置的盖子。
本装置在彼此独立的设备单元中分别完成秸秆的热解和炭化过程， 提 高了热解炭化效率。 使用时， 将农作物秸秆送入热解池， 利用秸秆的可燃 特性引燃秸秆， 通过秸秆自燃所产生的热量， 将秸秆干燥、 预热及部分热 解， 在此过程中， 根据秸秆含水量的不同及秸秆种类的不同， 控制供氧管 道的开合程度， 以达到迅速升温并有效干燥、 预热秸秆， 同时控制部分热 解程度确保秸秆不被过度热解成灰； 之后翻动翻板式炉箅将秸秆翻入进入 热解池下部， 在热解池中的分供氧口下部秸秆在缺氧状态下进行进一步热 解， 热解炭化过程所产生的 CO、 H2、 CnHm等可燃气体进入热解池分供氧 口以上空间进行二次燃烧， 以提高热解池的温度， 秸秆在结束热解池中的 热解过程后， 通过出料口将秸秆送入炭化池加盖带有单向通气装置的盖子 隔氧密闭， 根据秸秆炭的用途不同， 确定在炭化池中不同的炭化时间。
本发明还包括设置于热解池上方的烟气收集罩， 烟气收集罩通过烟道 与沉降室连通， 沉降室中设有一级或多级隔板， 沉降室一端顶部与烟道连 通， 沉降室另一端顶部开有排气口， 排气口下端连接油液收集罩， 油液收 集罩下方设有油液收集桶。
隔板只有一端与沉降室连接， 第一级隔板的上端与沉降室顶端连接， 第二级隔板与沉降室底部连接， 依此类推。 农作物秸秆热解炭化过程中的 烟气通过烟气收集罩及烟道进入沉降室一端， 再从隔板下方进入另一端， 最后从沉降室末端顶部的排气口排出， 通过这一路径， 使烟气的行程加大， 流速减缓， 同时也降低了烟气温度， 烟气中的可悬浮颗粒物沉降于沉降室 底部。 油液收集罩安装在沉降室末端排气口下端， 烟气通过袖液收集罩排 入大气， 进入沉降室的的烟气自然冷凝后， 其中所含的木焦油、 秸秆醋液 被油液收集罩吸附。
与现有技术相比， 本发明具有以下特点： （1 ) 热解过程中根据秸秆类 型的不同及秸秆含水分的差异， 控制氧气供给， 使秸秆在热解池中高效干 燥、 预热、 热解。 （2) 将农作物秸秆的热解和炭化过程分离， 由不同的设 备单元中完成， 极大地提高了热解炭化效率。 （3 ) 组合式结构设计使秸秆 热解炭化设备便于运输至秸秆产地， 快速组装生产， 解决了秸秆热解炭化 装置超大无法运输、 移动的难题。 （4) 便于拆分转运， 根据秸秆分布的情 况， 适时将秸秆热解炭化设备拆分转运至合理的工作区域， 以降低因秸秆 运输而产生的高昂运费， 在秸秆炭化实施地点， 将设备单元通过底板、 支 架、 紧固件进行快速组装， 在某一工作区域炭化结束后， 将设备拆分成基 本基本并运输至转向另一工作地点组装进行秸秆炭化。 （5 ) 秸秆热解过程 采用了烟气沉降室， 烟气流中的可悬浮颗粒物通过沉降室中的装置沉降于 沉降室底部， 木焦油及秸秆醋液经自然冷凝后附着于油液收集罩上， 流入 油液收集桶中收集， 尾气无害化排入大气， 确保生产过程环保无污染。
采用本发明生产的产品秸秆炭应用广泛， 用于加工生产农村居民用固 体燃料以替代化石燃料； 用于土壤改良， 提高土壤含水量、 透气性， 增加 土壤有机质含量， 以提高农作物产量， 减少农作物病虫害的发生； 用于沼 气生产原料秸秆的预处理， 使秸秆体积减小， 便于运输及储存， 使沼气生 产更具经济性和安全性。
附图说明
图 1为本发明的结构示意图。
图 2为热解池的结构示意图。
图 3为图 2的俯视图。
图中， 1一热解池， 2—炭化池， 3—供氧管道， 4一进氧口， 5—蝶阀， 6—分供氧口， 7—炉箅， 8—热解池出料口， 9一烟气收集罩， 10—烟道， 11一沉降室， 12—隔板， 13—排气口， 14一油液收集罩， 15—油液收集桶， 16—中空轴， 17—中空轴分供氧口， 18—火种台， 19一支架， 20—可升降 托板， 21—轨道。
具体实施方式
以下结合附图对本发明做进一步说明。
本发明所述的一种组合式农作物秸秆制炭方法， 热解过程中采用调节 氧气供给的方式控制热解过程， 热解和炭化分别在独立的热解池 1 和炭化 池 2中进行， 秸秆在热解池 1中完成热解过程后再进入炭化池 2进行炭化。
与以上方法相适应， 本发明所述的一种组合式农作物秸秆制炭装置， 包括热解池 1、 炭化池 2和可控式供氧管道 3， 供氧管道 3的进氧口 4处设 有供氧管道控制蝶阀 5，连接于可控式供氧管道 3上的分供氧口 6与热解池 1相通，热解池 1和炭化池 2为两个独立的设备单元， 热解池 1内部设有一 层或多层翻板式炉箅 7， 炭化池 2设于热解池出料口 8的下方， 炭化池（2) 带有单向通气装置的盖子。 热解池 1装配于支架 19上， 炭化池 2位于热解池 1下部的可升降托板 20上， 托板 20置于轨道 21上， 炉箅 7通过轴固定在热解池 1壁上， 供氧 管道蝶阀 5用于控制进氧口 4的开启和关闭，可控供氧管道 3设于热解池 1 炉箅 7下方沿热解池 1外壁并与热解池 1外部联通， 炭化池 2上带有的单 向通气装置盖子， 当压力过大时， 盖子被顶起释放出气体。 一个热解池 1 可对应设置一个或多个炭化池 2，炭化池 2除具有炭化功能外， 还可用于转 用炭化产品， 可以保证热解过程连续进行。 在可控供氧管道 3 上分布着与 热解池 1内部相通的分供氧口 6， 因热解池 1内秸秆燃烧产生热气上升，使 热解池 1内外产生气压差，.此时， 如果开启联通热解池 1外部的蝶阀 5， 热 解池 1外部的空气会由于负压的作用通过供氧管道 3进入热解池 1，以达到 助燃的作用。 秸秆进入热解池 1后引燃初期， 完全打开进氧口 4以迅速提 高热解池内温度， 使秸秆迅速干燥、 预热。 当温度达到 200-850°C时， 逐步 减小进氧口 4的开启程度， 减少氧气进入热解池 1， 以避免过度供氧造成秸 秆过度热解成灰。
本发明还包括设置于热解池 1上方的烟气收集罩 9，烟气收集罩通过支 架 19置于热解池 1上部， 烟气收集罩 9通过烟道 10与沉降室 11连通， 沉 降室 11中设有一级或多级隔板 12， 沉降室 11一端顶部与烟道 10连通， 沉 降室 11另一端顶部开有排气口 13， 排气口 13下端连接油液收集罩 14， 油 液收集罩 14下方设有油液收集桶 15。 油液收集罩 15为锥筒形， 表面上分 布有通孔。 隔板 12只有一端与沉降室壁 11连接， 而另一端与沉降室 11壁 分离， 如第一级隔板的上端与沉降室顶端连接， 第二级隔板与沉降室底部 连接， 依此类推， 在沉降室 11内形成烟气通道。
所述的分供氧口 6设置为与翻板式炉箅 7对应的一层或多层， 并分层 独立控制， 分供氧口 6的位置低于或齐平于对应的翻板式炉箅 7所在平面， 使每一层炉箅 7上的秸秆都能得到充分的氧气。
为了在现有结构的基础上进一步提高氧气的利用效率，在翻板式炉箅 7 固定在中空轴 16上， 中空轴 16与供氧管道 3连通， 中空轴 16上开有中空 轴分供氧口 17， 使炉箅上的中空轴也成为供氧部位。 翻板式炉箅 Ί下方设有火种台 18，火种台 18是固定于热解池壁上的平 台或盘形结构， 在热解过程中， 极少量燃烧的秸秆落入火种台 18, 使后续 送入热解池的秸秆被迅速引燃。
本发明由热解池 1、 炭化池 2、 烟气收集罩 9及沉降室 11 四个主要设 备单元和其他辅助装置构件组成。 使用时， 将干燥易燃的农作物秸秆送入 热解池 1 中的翻板式炉箅 7上并引燃。 供氧是在秸秆燃烧热气上升的过程 中， 由于产生负压而通过供氧管道 3向热解池 1 自动补充充足的氧气， 迅 速提高热热解池 1 内温度， 使秸秆迅速干燥、 预热并部分热解。 在秸秆利 用自身热量进行热解的初期， 根据秸秆种类的不同及含水分的不同， 适时 调整进氧口 4上的供氧管道蝶阀 5的开启程度， 在确保高效利用秸秆自热 迅速提高温度的前提下， 避免过度供氧造成秸秆过度热解成灰。 秸秆通过 在热解池内的迅速干燥、 预热及部分热解后， 翻动翻板式炉箅 7， 使炉箅 7 上的所有秸秆落入热解池 1 下部， 在此过程中， 极少量燃烧的秸秆落入火 种台 18， 使后续送入热解池 1 的秸秆被迅速引燃； 而大部分落入热解池 1 下部的秸秆在高温隔氧状态下继续升温至热解温度， 此过程避免了秸秆的 部分纤细组分在高温状态因氧气供给过量而燃烧成灰。 在剧烈的热解炭化 过程， 构成秸秆的主要成分： 全部的纤维素、 半纤维素及部分木质素在此 阶段完成热解炭化。 在经过热解升温过程后， 秸秆通过热解池出料口 8进 入炭化池 2 中， 并立即加盖带有单向通气装置的盖子加以密闭隔氧， 利用 秸秆自热继续炭化， 根据秸秆炭的不同用途， 最终确定秸秆在炭化池 2 中 的炭化时间。 热解过程中的烟气通过烟气收集罩 9及烟道进入沉降室 11， 沉降室 11 中在烟气流动方向纵向设置隔板 12将沉降室分开， 能有效减缓 烟气流速， 降低烟气温度， 并使部分烟气中的可悬浮颗粒物沉降于沉降室 11底部， 并集中收集处理。 农作物秸秆热解炭化过程中存在于烟气中的木 焦油及秸秆醋液经沉降室逐级自然冷凝后附着于油液收集罩 14上， 流入油 液收集桶 15中， 并集中收集回收另行处理， 尾气通过排气口无害化排入大 气。

Claims

权 利 要 求
1、 一种农作物秸秆制炭方法， 包括热解和炭化过程， 其特征在于： 热 解过程中采用调节氧气供给的方式控制热解过程， 热解和炭化分别在独立 的热解池 （1) 和炭化池 （2) 中进行， 秸秆在热解池 （1) 中完成热解过程 后再进入炭化池 （2) 进行炭化。
2、 实现权利要求 1所述方法的农作物秸秆制炭装置， 其特征在于： 包 括热解池 （1)、 炭化池 （2) 和可控式供氧管道 （3)， 供氧管道 （3) 的进 氧口 （4) 处设有供氧管道控制蝶阀 （5)， 连接于可控式供氧管道 （3) 上 的分供氧口 （6) 与热解池 （1) 相通， 热解池 （1) 和炭化池 （2) 为两个 独立的设备单元， 热解池 （1) 内部设有一层或多层翻板式炉箅 （7)， 炉箅 连接于一根或多根轴上， 炭化池 （2) 设于热解池出料口 （8) 的下方， 炭 化池 （2) 带有单向通气装置的盖子。
3、 根据权利要求 2所述的农作物秸秆制炭装置， 其特征在于： 还包括 设置于热解池（1)上方的烟气收集罩（9)， 烟气收集罩（9)通过烟道（10) 与沉降室 （11) 连通， 沉降室 （11) 中设有一级或多级隔板 （12)， 沉降室
(11) 一端顶部与烟道 （10) 连通， 沉降室 （11) 另一端顶部开有排气口 (13)， 排气口 （13) 下端连接油液收集罩 （14)， 油液收集罩 （14) 下方 设有油液收集桶 （15)。
4、 根据权利要求 2或 3所述的农作物秸秆制炭装置， 其特征在于： 所 述的分供氧口 （6) 设置为与翻板式炉箅 （7) 对应的一层或多层并分层独 立控制， 分供氧口 （6) 的位置低于或齐平于对应的翻板式炉箅 （7) 所在 平面。
5、 根据权利要求 2或 3所述的农作物秸秆制炭装置， 其特征在于： 翻 板式炉箅 （7) 固定在中空轴 （16) 上， 中空轴 （15) 与供氧管道 （3) 连 通， 中空轴 （15) 上开有中空轴分供氧口 （17)。
6、 根据权利要求 4所述的农作物秸秆制炭装置， 其特征在于： 翻板式 炉箅 （7) 固定在中空轴 （16) 上， 中空轴 （15) 与供氧管道 （3) 连通， 中空轴 （15) 上开有中空轴分供氧口 （17)。
7、根据权利要求 2或 3或 6所述的农作物秸秆制炭装置，其特征在于： 翻板式炉箅 （7) 下方设有火种台 （18)。
8、 根据权利要求 5所述的农作物秸秆制炭装置， 其特征在于： 翻板式 炉箅 （7) 下方设有火种台 （18)。
PCT/CN2011/000265 2010-02-23 2011-02-21 农作物秸秆制炭方法及装置 WO2011103768A1 (zh)

Priority Applications (6)

Application Number Priority Date Filing Date Title
BR112012021187A BR112012021187A2 (pt) 2010-02-23 2011-02-21 método e dispositivo para carbonificação de palhada de colheita
US13/579,147 US9321966B2 (en) 2010-02-23 2011-02-21 Method for carbonization of crop straws
EP11746810.8A EP2540803B1 (en) 2010-02-23 2011-02-21 Method for preparing char from crop-straw and apparatus therefor
RU2012133192/05A RU2573014C2 (ru) 2010-02-23 2011-02-21 Способ производства угля из соломы и устройство для обугливания соломы
ZA2012/05861A ZA201205861B (en) 2010-02-23 2012-08-03 Method and device for carbonification of crop straws
US15/136,514 US10273412B2 (en) 2010-02-23 2016-04-22 Method and device for carbonization of crop straws

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN201010114478A CN101775299A (zh) 2010-02-23 2010-02-23 农作物秸秆限氧自热式热解快速制炭设备
CN201010114478.9 2010-02-23

Related Child Applications (2)

Application Number Title Priority Date Filing Date
US13/579,147 A-371-Of-International US9321966B2 (en) 2010-02-23 2011-02-21 Method for carbonization of crop straws
US15/136,514 Division US10273412B2 (en) 2010-02-23 2016-04-22 Method and device for carbonization of crop straws

Publications (1)

Publication Number Publication Date
WO2011103768A1 true WO2011103768A1 (zh) 2011-09-01

Family

ID=42511887

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2011/000265 WO2011103768A1 (zh) 2010-02-23 2011-02-21 农作物秸秆制炭方法及装置

Country Status (7)

Country Link
US (2) US9321966B2 (zh)
EP (1) EP2540803B1 (zh)
CN (2) CN101775299A (zh)
BR (1) BR112012021187A2 (zh)
RU (1) RU2573014C2 (zh)
WO (1) WO2011103768A1 (zh)
ZA (1) ZA201205861B (zh)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2022268234A1 (zh) * 2021-06-25 2022-12-29 王晓光 一种秸秆快速制炭及烟气烟尘回收处理装置及方法

Families Citing this family (50)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7998316B2 (en) 2009-03-17 2011-08-16 Suncoke Technology And Development Corp. Flat push coke wet quenching apparatus and process
US10751885B2 (en) 2012-02-16 2020-08-25 Biochar Now, Llc Gripper assembly for portable biochar kiln
US11135728B2 (en) 2012-02-16 2021-10-05 Biochar Now, Llc Lid assembly for portable biochar kiln
US10370593B2 (en) * 2012-02-16 2019-08-06 Biochar Now, Llc Controlled kiln and manufacturing system for biochar production
US10160911B2 (en) 2012-02-16 2018-12-25 Biochar Now, Llc Exhaust system for a biochar kiln
US9752078B2 (en) 2012-03-11 2017-09-05 Biochar Now, Llc Airflow control and heat recovery in a managed kiln
US9359554B2 (en) 2012-08-17 2016-06-07 Suncoke Technology And Development Llc Automatic draft control system for coke plants
US9243186B2 (en) 2012-08-17 2016-01-26 Suncoke Technology And Development Llc. Coke plant including exhaust gas sharing
US9169439B2 (en) 2012-08-29 2015-10-27 Suncoke Technology And Development Llc Method and apparatus for testing coal coking properties
WO2014105065A1 (en) 2012-12-28 2014-07-03 Suncoke Technology And Development Llc. Vent stack lids and associated systems and methods
WO2014105063A1 (en) 2012-12-28 2014-07-03 Suncoke Technology And Development Llc. Systems and methods for maintaining a hot car in a coke plant
US10883051B2 (en) 2012-12-28 2021-01-05 Suncoke Technology And Development Llc Methods and systems for improved coke quenching
US9238778B2 (en) 2012-12-28 2016-01-19 Suncoke Technology And Development Llc. Systems and methods for improving quenched coke recovery
CN104902984B (zh) 2012-12-28 2019-05-31 太阳焦炭科技和发展有限责任公司 用于去除排放物中的汞的系统和方法
US10047295B2 (en) 2012-12-28 2018-08-14 Suncoke Technology And Development Llc Non-perpendicular connections between coke oven uptakes and a hot common tunnel, and associated systems and methods
US9273249B2 (en) * 2012-12-28 2016-03-01 Suncoke Technology And Development Llc. Systems and methods for controlling air distribution in a coke oven
US9273250B2 (en) 2013-03-15 2016-03-01 Suncoke Technology And Development Llc. Methods and systems for improved quench tower design
CN105916965B (zh) 2013-12-31 2021-02-23 太阳焦炭科技和发展有限责任公司 用于焦炉脱碳的方法及相关系统和装置
AU2015308678B2 (en) 2014-08-28 2017-06-29 Suncoke Technology And Development Llc Method and system for optimizing coke plant operation and output
CA2961207C (en) 2014-09-15 2023-04-18 Suncoke Technology And Development Llc Coke ovens having monolith component construction
WO2016109704A1 (en) 2014-12-31 2016-07-07 Suncoke Technology And Development Llc Multi-modal beds of coking material
BR112017014428B1 (pt) 2015-01-02 2022-04-12 Suncoke Technology And Development Llc Método para otimizar a operação de uma usina de coque e forno de coque
US11060032B2 (en) 2015-01-02 2021-07-13 Suncoke Technology And Development Llc Integrated coke plant automation and optimization using advanced control and optimization techniques
WO2016126601A1 (en) 2015-02-06 2016-08-11 Biocharnow, Llc Contaminant removal from water bodies with biochar
CN104987871A (zh) * 2015-06-17 2015-10-21 湖南冠威环境工程发展有限公司 生活垃圾小型化连续式自加热可移动卧式干馏机
AU2016382975A1 (en) 2015-12-28 2018-07-19 Suncoke Technology And Development Llc Method and system for dynamically charging a coke oven
CN106931446A (zh) * 2015-12-31 2017-07-07 未名生物环保集团有限公司 垃圾高效环保热解装置
US10385273B2 (en) 2016-04-03 2019-08-20 Biochar Now, Llc Biochar kiln
MX2018000954A (es) 2016-06-03 2018-06-07 Suncoke Tech & Development Llc Metodos y sistemas para generar automaticamente una accion correctiva en una instalacion industrial.
BR112019024618B1 (pt) 2017-05-23 2022-05-03 Suncoke Technology And Development Llc Sistema e método para reparar um forno de coque
BR102017021185B1 (pt) * 2017-10-02 2022-07-26 Vallourec Tubos Do Brasil S.A. Método de reaproveitamento energético de gases de carbonização para produção contínua de carvão vegetal, sistema e reator para produção contínua de carvão vegetal para produção contínua de carvão vegetal
CN107805515A (zh) * 2017-11-16 2018-03-16 建始惠万农生物科技有限公司 一种秸秆碳化装置
BR112021012766B1 (pt) 2018-12-28 2023-10-31 Suncoke Technology And Development Llc Descarbonização de fornos de coque e sistemas e métodos associados
CA3125337C (en) 2018-12-28 2022-06-21 Suncoke Technology And Development Llc Particulate detection for industrial facilities, and associated systems and methods
BR112021012455B1 (pt) 2018-12-28 2023-10-24 Suncoke Technology And Development Llc Forno de coque
CA3125279A1 (en) 2018-12-28 2020-07-02 Suncoke Technology And Development Llc Improved oven uptakes
BR112021012725B1 (pt) 2018-12-28 2024-03-12 Suncoke Technology And Development Llc Método para reparar um vazamento em um forno de coque de uma coqueria, método de reparo da superfície de um forno de coque configurado para operar sob pressão negativa e tendo um piso de forno, uma câmara de forno e uma chaminé única e método de controle de ar descontrolado em um sistema para carvão de coque
WO2020140095A1 (en) 2018-12-28 2020-07-02 Suncoke Technology And Development Llc Spring-loaded heat recovery oven system and method
WO2020142391A1 (en) 2018-12-31 2020-07-09 Suncoke Technology And Development Llc Methods and systems for providing corrosion resistant surfaces in contaminant treatment systems
BR112021012412A2 (pt) 2018-12-31 2021-09-08 Suncoke Technology And Development Llc Sistemas e métodos aprimorados para utilizar gás de combustão
US11254875B2 (en) * 2019-06-27 2022-02-22 Paul S. Anderson Covered cavity kiln pyrolyzer
CN110776938A (zh) * 2019-09-29 2020-02-11 中原环资科技有限公司 一种热解碳提纯工艺方法
CN111218291B (zh) * 2020-03-09 2021-05-07 中国农业科学院农业环境与可持续发展研究所 一种热解炭化催化一体化方法
EP4146767A1 (en) 2020-05-03 2023-03-15 Suncoke Technology and Development LLC High-quality coke products
CN112920816A (zh) * 2021-03-02 2021-06-08 济源润万家农业科技有限公司 一种烟气回用内热式生物质炭化炉
EP4337605A2 (en) * 2021-05-14 2024-03-20 Cummins, Inc. Enhancements for low cost autothermal pyrolyzer
CA3211286A1 (en) 2021-11-04 2023-05-11 John Francis Quanci Foundry coke products, and associated systems, devices, and methods
US11946108B2 (en) 2021-11-04 2024-04-02 Suncoke Technology And Development Llc Foundry coke products and associated processing methods via cupolas
CN114686271A (zh) * 2022-03-21 2022-07-01 宁波宗吉科技有限公司 一种生产竹炭的大型生物质炭化气化炉及其生产方法
CN115109606B (zh) * 2022-07-06 2023-09-08 山东省红森林新材料科技有限公司 一种生物质废弃物制取纯氢及多联产耦合系统

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1326423A (zh) * 1998-10-28 2001-12-12 株式会社荏原制作所 废物碳化方法
EP1312662A2 (en) * 2001-05-07 2003-05-21 Cirad-Foret Biomass gasification process, and apparatus, and their applications
CN101195757A (zh) * 2008-01-02 2008-06-11 韩璋鑫 生产生物质干馏炭和生物质燃气的方法及快速热解炭化炉
CN101565637A (zh) * 2009-05-31 2009-10-28 肖国雄 一种低成本生物油生产方法

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1395866A (en) * 1921-11-01 Canada
BE458091A (zh) *
US1190006A (en) * 1915-06-11 1916-07-04 Free Stump Remover Mfg Company Process of and apparatus for reducing stumps.
FR903723A (fr) * 1943-11-19 1945-10-12 Procédé et dispositifs pour la carbonisation continue du menu bois tel que ramilles, sarments et autres substances
US2885338A (en) * 1953-12-04 1959-05-05 Socony Mobil Oil Co Inc Process and apparatus for retorting of oil shale
US3875317A (en) * 1971-09-17 1975-04-01 Stuart R Ferguson Waste conversion process
DE3030593A1 (de) * 1980-08-11 1982-03-11 Michel-Kim, Herwig, 1000 Berlin Verfahren und vorrichtungen zur wirtschaftlichen und umweltfreundlichen nutzung von bio-masse, wie agrar- und forstabfaellen, und von organischen abfaellen, wie altreifen, kunststoffe, papier u.dgl.
DE4330884A1 (de) * 1993-09-13 1995-03-16 Bayer Ag Verfahren zur Verwertung von Klärschlämmen
EP1473351A4 (en) * 2002-01-10 2007-12-05 Shigeo Muramatsu PROCESS FOR PRODUCING SMOKE-FREE POROUS CHARCOAL AND SYSTEM FOR PRODUCING SAME
JP2007146016A (ja) * 2005-11-29 2007-06-14 Kochi Univ Of Technology 木質材の炭化炉
CN101020826B (zh) * 2007-03-09 2010-11-17 华东理工大学 厨余垃圾的焦化处理方法及其处理装置
CN101245250A (zh) * 2008-03-19 2008-08-20 北京林业大学 木质化生物质材料能源化综合利用的方法
DE102009030013A1 (de) * 2009-04-27 2010-11-04 Schottdorf, Bernd, Dr. Vorrichtung, deren Verwendung, Verfahren und System zur kontinuierlichen Umwandlung von Biomasse

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1326423A (zh) * 1998-10-28 2001-12-12 株式会社荏原制作所 废物碳化方法
EP1312662A2 (en) * 2001-05-07 2003-05-21 Cirad-Foret Biomass gasification process, and apparatus, and their applications
CN101195757A (zh) * 2008-01-02 2008-06-11 韩璋鑫 生产生物质干馏炭和生物质燃气的方法及快速热解炭化炉
CN101565637A (zh) * 2009-05-31 2009-10-28 肖国雄 一种低成本生物油生产方法

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2022268234A1 (zh) * 2021-06-25 2022-12-29 王晓光 一种秸秆快速制炭及烟气烟尘回收处理装置及方法

Also Published As

Publication number Publication date
CN102134497B (zh) 2013-08-21
US20160326437A1 (en) 2016-11-10
CN101775299A (zh) 2010-07-14
CN102134497A (zh) 2011-07-27
RU2012133192A (ru) 2014-03-27
EP2540803B1 (en) 2017-09-27
US10273412B2 (en) 2019-04-30
EP2540803A1 (en) 2013-01-02
EP2540803A4 (en) 2015-08-19
RU2573014C2 (ru) 2016-01-20
US9321966B2 (en) 2016-04-26
ZA201205861B (en) 2013-05-29
BR112012021187A2 (pt) 2016-05-17
US20120305380A1 (en) 2012-12-06

Similar Documents

Publication Publication Date Title
WO2011103768A1 (zh) 农作物秸秆制炭方法及装置
US10253263B2 (en) Method of continuous pyrolysis and carbonization of agricultural and forestry biomass
CN110079337A (zh) 一种生物质热解气再循环利用的炭化炉及生物质炭化方法
CN201339016Y (zh) 一种锯屑、糠醛渣碳化装置
CN105062521B (zh) 一种回转式连续热解秸秆炭化炉
CN107828435A (zh) 一种机制高温竹炭的制备装置及其炭化工艺
CN104031666A (zh) 一种带有烟气余热利用功能的竹材炭化窑炉
CN201362687Y (zh) 一种秸秆炭化装置
CN103773404B (zh) 一种组合式多联产生物质快速炭化设备及其制炭方法
CN211255815U (zh) 一种小柜式垃圾低温热解系统
CN101570691B (zh) 生物质炭化、汽化设备及工艺
CN204125311U (zh) 一种二段式污泥燃气化处理装置
CN116179243A (zh) 生物质热裂解设备及方法
US20110078953A1 (en) A method and plant of production of combustible gas using biomass
CN107022363A (zh) 一种连续式生物质热解气逆流回用炭气联产设备
CN202865166U (zh) 一种带有烟道管的干馏炭化炉
CN206278918U (zh) 一种热解炉和耙式炉联合制备活性炭的系统
CN210241577U (zh) 一种小柜式垃圾低温热解炉
CN110397925B (zh) 一种小柜式垃圾低温热解系统及其工艺
CN201634626U (zh) 农作物秸秆限氧自热式热解快速制炭设备
CN110240914A (zh) 一种竖井式列管炭化炉
CN206970530U (zh) 一种酒糟处理系统
CN203768295U (zh) 一种组合式多联产生物质快速炭化设备及其制炭方法
CN110878223B (zh) 一种生物质燃气高效气化装置
CN219772040U (zh) 一种序批连续式梯级自供热原木炭烧制设备

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 11746810

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: 13579147

Country of ref document: US

NENP Non-entry into the national phase

Ref country code: DE

REEP Request for entry into the european phase

Ref document number: 2011746810

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 2011746810

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 2012133192

Country of ref document: RU

REG Reference to national code

Ref country code: BR

Ref legal event code: B01A

Ref document number: 112012021187

Country of ref document: BR

ENP Entry into the national phase

Ref document number: 112012021187

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20120823