WO2011054304A1 - 一种气载体内热式低阶煤提质工艺 - Google Patents

一种气载体内热式低阶煤提质工艺 Download PDF

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WO2011054304A1
WO2011054304A1 PCT/CN2010/078421 CN2010078421W WO2011054304A1 WO 2011054304 A1 WO2011054304 A1 WO 2011054304A1 CN 2010078421 W CN2010078421 W CN 2010078421W WO 2011054304 A1 WO2011054304 A1 WO 2011054304A1
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coal
low
gas
reactor
raw coal
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郭彩应
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Hunan Datang Xianyi Technology Co Ltd
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Hunan Datang Xianyi Technology Co Ltd
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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
    • 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
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
    • 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
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B11/00—Machines or apparatus for drying solid materials or objects with movement which is non-progressive
    • F26B11/18—Machines or apparatus for drying solid materials or objects with movement which is non-progressive on or in moving dishes, trays, pans, or other mainly-open receptacles
    • F26B11/20—Machines or apparatus for drying solid materials or objects with movement which is non-progressive on or in moving dishes, trays, pans, or other mainly-open receptacles with stirring devices which are held stationary

Definitions

  • the invention relates to a process for performing internal heat type low rank coal upgrading by using a spent oxygen hot gas carrier. Background technique
  • Low-rank coal includes peat, lignite and long-flame coal, gas coal, weakly cohesive coal and other sub-bituminous coal, accounting for about 50% of the world's coal reserves. Similarly, low-rank coal is also extremely rich in China's reserves, accounting for about China's coal. More than 60% of reserves. Mainly distributed in Yunnan, Inner Mongolia, Northeast, Sichuan and other provinces. It is characterized by high water content, generally accounting for more than 20% (receiving base); high volatile content, about 30 ⁇ 50% (dry ashless base); low calorific value, 2500 ⁇ 4500 kcal / kg.
  • the development of low-rank coal upgrading process is mainly two: dry upgrading and low temperature retorting (pyrolysis) Two kinds of upgrading process.
  • the drying and upgrading process can only remove the moisture in the coal to a certain extent, and cannot achieve the purpose of complete or most of the removal.
  • the dried coal is prone to rehydration and spontaneous combustion, so it is low.
  • the development direction of the step coal upgrading process is mainly low temperature dry distillation upgrading.
  • Chinese patent CN201053004Y introduces a retorting of bituminous coal and bituminous coal using a rotary kiln
  • Chinese patent CN1966612A discloses a process technology for dry-strengthening of weakly cohesive coal by an internal heat type vertical furnace using a gas carrier, which can only be used for upgrading the bituminous coal with low water content, and requires high coal type. It is difficult to achieve diversification of the treatment of coal; and in order to ensure heat transfer efficiency and gas circulation, the amount of coal to be treated is not large, and it is difficult to achieve industrial scale expansion.
  • Chinese patent CN1847364 A discloses a process technology for pyrolysis of a thermoset carrier using a circulating fluidized bed and a rotary kiln, which uses a semi-coke to heat a solid heat carrier in a circulating fluidized bed and then circulates to a rotary kiln.
  • Low-order coal is subjected to pyrolysis and dry distillation.
  • the process is simple, the thermal efficiency is high, and a large yield of high calorific value gas and coal tar is obtained, but the production process is limited by the gas separation efficiency, and the gas and tar products are high in dust, the pipeline
  • the problem of blockage has not been completely solved, so the degree of industrialization is not high, and the production process has a great impact on the environment. Summary of the invention
  • the technical problem to be solved by the invention is to provide a heat carrier low-rank coal upgrading process in a gas carrier, which not only has a single process, is easy to control, but also has high thermal efficiency and low energy consumption ratio, and can be used for upgrading various low-rank coals.
  • a heat carrier low-rank coal upgrading process in a gas carrier which not only has a single process, is easy to control, but also has high thermal efficiency and low energy consumption ratio, and can be used for upgrading various low-rank coals.
  • the present invention provides a gas carrier internal thermal low-rank coal upgrading process, the process comprising the following steps:
  • hypoxic heating gas enters from the hot gas inlet disposed under the reactor, and is directly contacted with the coal sample through the perforation on the furnace for heat transfer, causing drying or pyrolysis reaction;
  • the treated coal sample is pushed to the discharge port by a plough mechanical agitator fixedly disposed above the rotary furnace, and the hot gas exhaust gas is discharged through the exhaust outlet.
  • the raw coal particles entering the reactor have a particle size distribution of 6 to 50 mm, and the oxygen content of the imported hypoxic heating gas is less than 1%.
  • the invention uses hypoxic circulating flue gas as a heat source for low-order coal retorting, and the flue gas directly exchanges heat with solid coal, which has high thermal efficiency and low energy consumption ratio;
  • the process technology has good adaptability and can be used to upgrade a variety of low-rank coal types
  • the raw coal particle size requirement is low, the soot content in the process gas is low, and the environment is protected, which also alleviates the problem that the dust and tar are mixed and easy to block the pipeline during long-term operation;
  • FIG. 1 is a schematic view showing the structure and process of a gas carrier internal low-grade coal upgrading device of the present invention.
  • the raw material coal having a particle size distribution of 6 to 50 mm which has been pulverized and sieved is fed into the rotary hearth 5 of the reactor 2 through the raw coal feed slip pipe 1, and the falling point of the feed slip pipe is Furnace
  • the distance between the crucibles is the thickness of the treated coal seam, and the oxygen-containing heating gas having an oxygen content of less than 1% enters from the hot gas inlet 4 disposed under the reactor 2, and is directly contacted with the coal sample 3 through the perforation on the furnace.
  • Example 1 the pulverized sieving treatment to 15-50mm, about 25 tons of water containing 14.25%, the volatile matter is 25.43%, the calorific value is 5500 kcal / kg weakly bonded sub-bituminous coal first sent to the gas carrier for thermal drying
  • the drying gas is a hypoxic hot gas having an oxygen content of 0.8% and a temperature of 320 ° C.
  • Example 2 the pulverized sieving treatment to 15-50 mm, about 22 tons of water containing 38.5%, the volatile matter is 23.38%, and the calorific value of 3400 kcal/kg of lignite is first sent into the gas carrier in the thermal drying reactor 2,
  • the drying gas is a hypoxic hot gas with an oxygen content of 0.6% and a temperature of 327 °C.
  • a 2% water sample is introduced into the gas carrier internal thermal pyrolysis reactor 2 for low-temperature carbonization, and the dry distillation gas is 530 ° C.
  • the hot gas is treated with 20% dry distillation to obtain a product coal with a yield of 44.5% and a calorific value of 6100 kcal/kg, and 4% of the coal tar is recovered, and the dry distillation tail gas contains 300 g/Nm 3 (after the cyclone). .
  • Example 3 the pulverized sieving treatment to 6-50 mm, about 28 tons of water containing 8.31%, the volatile matter is 30.56%, and the calorific value is 6100 kcal/kg weakly bonded sub-bituminous coal into the gas carrier for thermal pyrolysis
  • the reactor is subjected to low-temperature dry distillation, and the dry distillation gas is 660 ° C anoxic hot gas. After 25 minutes of dry distillation, a product yield of 66.9%, a calorific value of 7100 kcal/kg of product coal, and 8.2% of coal tar are recovered.
  • the dry distillation tail gas contains 140mg/Nm 3 (after the cyclone).

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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)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Description

一种气载体内热式低阶煤 工艺 技术领域
本发明涉及一种利用乏氧热气载体进行内热式的低阶煤提质的工艺。 背景技术
目前我国的煤炭资源的开采和利用仍以无烟煤和烟煤为主， 随着我国对 能源需求的不断增加， 以及无烟煤和烟煤资源过度开采造成的资源紧张， 而 通过对低阶煤进行提质转化代替高阶煤，緩解能源需求压力显得越来越重要。
低阶煤包括泥煤、 褐煤和长焰煤、 气煤、 弱粘结煤等次烟煤， 约占世界 煤炭资源储量的 50%, 同样低阶煤在我国储量也极其丰富， 大约占我国煤炭 储量的 60%以上。 主要分布在云南、 内蒙古、 东北、 四川等省份。 其特点是 含水量高， 一般占 20%以上（收到基）； 挥发份高， 约在 30 ~ 50% (干燥无灰 基） ； 热值低， 在 2500 ~ 4500千卡 /公斤。
针对低阶煤反应活性高、 易自燃、 不易长途运输、 含水量大、 热值低等 的缺点， 低阶煤提质工艺的开发的主要是两种： 干燥提质和低温干馏（热解） 提质工艺两种。其中干燥提质工艺一方面只能将煤中水分进行一定程度脱除， 不能达到完全或绝大部分脱除的目的， 另一方面干燥后的煤极易发生复吸水 和自燃的现象， 所以低阶煤的提质工艺发展方向主要是低温干馏提质。
通过低温干馏（热解）对低阶煤进行提质的研究早在上世纪初就开始进 行， 上世纪 80年代前后， 达到高峰， 国内外开发了许多具有各自鲜明特点的 工艺，例如：国外具有代表性的有德国的 L-R (鲁奇-鲁尔）固载体低温干馏工艺， 美国油页岩公司的 Toscoal工艺， 美国西方研究公司 Garrett工艺， 美国 COED 工艺； 国内现有具有代表性的有陕西三江集团的 SJ, 大连理工大学的 DG固载 体工艺， 煤炭科学总院的回转炉工艺， 以及中国科学院的循环流化床锅炉联 用工艺。 由于无法解决真正褐煤含水高的问题， 用于褐煤干馏提质的成熟工 业化的技术较少， 大多集中在高挥发、 弱粘结次烟煤的干馏工艺。
中国专利 CN201053004Y介绍了一种使用回转炉进行次烟煤和烟煤干馏 提质处理的工艺技术， 该工艺虽处理煤量大， 可以实现规模化生产， 但是处 理低阶煤能力不高， 能耗大， 且对工厂建设要求高， 占地较大， 设备配套系 统复杂。
中国专利 CN1966612A中公开了一种使用气载体的内热式直立炉进行弱 粘结性煤干馏提质的工艺技术， 该工艺只能用于含水量较低的烟煤的提质加 工， 煤种要求高， 很难实现处理煤种的多样化； 且该工艺为了保证传热效率 和气体循环量， 处理煤量并不大， 难以实现工业规模的扩大化生产。
中国专利 CN1847364 A公开了一种利用循环流化床和回转窑进行热固载 体热解的工艺技术， 该工艺通过在循环流化床内使用半焦加热固体热载体， 然后循环到回转窑内对低阶煤进行热解干馏， 虽然工艺筒单， 热效率高， 并 获得较大收率的高热值煤气和煤焦油， 但是生产过程中受气粉分离效率的限 制， 气体和焦油产品含尘高， 管道堵塞问题没有彻底解决， 因此工业化程度 不高， 生产过程对环境影响大。 发明内容
本发明要解决的技术问题是提供一种气载体内热式低阶煤提质工艺， 不 仅工艺过程筒单、 易于控制， 而且热效率高、 能耗比低， 可用于提质多种低 阶煤煤种。
为了解决上述问题， 本发明提供的一种气载体内热式低阶煤提质工艺， 该工艺包括如下步骤：
1 )经过粉碎和筛分处理的原料煤经过原煤进料溜管加入到反应器底部的 旋转炉蓖中， 进料溜管的落点与炉蓖之间的距离为处理煤层厚度；
2 )乏氧加热气体从设置在反应器下方的热气体进口进入， 并通过炉蓖上 的凿孔与煤样直接接触进行传热， 发生干燥或热解反应；
3 )经过一定反应时间后， 随旋转炉蓖的转动， 处理后的煤样被固定设置 在旋转炉蓖上方的犁式机械搅拌器推至卸料口， 热气体尾气经过排气出口排 出。 优选地， 进入所述反应器的原煤颗粒粒度分布在 6 ~ 50mm, 进口乏氧加 热气体的含氧量小于 1%。
本发明具有如下优点：
1、 本发明使用乏氧循环烟气作为低阶煤干馏的热源， 烟气直接与固体煤 进行热交换， 热效率高、 能耗比低；
2、 工艺技术适应性好， 可用于提质多种低阶煤煤种；
3、 原煤粒度要求低， 工艺气中烟尘含量低， 保护环境， 也緩解了长期运 行中粉尘和焦油混合易堵塞管道的问题；
4、 工艺过程筒单、 易于控制， 产品丰富、 市场调节性高， 易于工业规模 化。 附图说明
图 1是本发明的气载体内热式低阶煤提质装置结构和工艺示意图。
1-原煤进料溜管
2-反应器
3-原煤煤样
4-热气体进口
5-旋转炉蓖
6-犁式机械搅拌器
74非气出口
8-卸料口
具体实施方式
如图 1所示，经过粉碎和筛分处理的颗粒粒度分布在 6 ~ 50mm的原料煤 经过原煤进料溜管 1加入到反应器 2的旋转炉蓖 5中， 进料溜管的落点与炉 蓖之间的距离为处理煤层厚度，含氧量在 1%以下的乏氧加热气体从设置在反 应器 2下方的热气体进口 4进入， 通过炉蓖上的凿孔与煤样 3直接接触进行 传热， 发生干燥或热解反应， 一定反应时间后， 随旋转炉蓖 5的转动， 处理 后的煤样被固定设置在旋转炉蓖 5上方的犁式机械搅拌器 6刮至卸料口 8, 进入到下一道工序， 热气体尾气经过排气出口 7排出。
下面通过具体示范例进行说明。
示范例 1 , 将经粉碎筛分处理至 15-50mm约 25吨的含水 14.25%, 挥发 份为 25.43% , 发热量为 5500大卡 /千克弱粘结性次烟煤首先送入气载体内热 式干燥反应器 2内， 干燥气为含氧量 0.8%、 温度 320 °C的乏氧热气体， 25min 后含水 3%的煤样进入气载体内热式热解反应器 2内进行低温干馏，干馏气为 600°C乏氧热气体， 经 20min干馏处理后获得产率为 69.9% , 发热量为 6990 大卡 /千克的产品煤， 并回收 6.4%的煤焦油， 干馏尾气中含尘 190mg/Nm3 (过 旋风器后） 。
示范例 2, 将经粉碎筛分处理至 15-50mm约 22吨的含水 38.5%, 挥发份 为 23.38% , 发热量为 3400大卡 /千克褐煤首先送入气载体内热式干燥反应器 2内， 干燥气为含氧量 0.6%、 温度 327 °C的乏氧热气体， 20min后含水 2%的 煤样进入气载体内热式热解反应器 2 内进行低温干馏， 干馏气为 530°C乏氧 热气体，经 20min干馏处理后获得产率为 44.5% ,发热量为 6100大卡 /千克的 产品煤， 并回收 4%的煤焦油， 干馏尾气中含尘 300g/Nm3 (过旋风器后） 。
示范例 3 , 将经粉碎筛分处理至 6-50mm约 28吨的含水 8.31% , 挥发份 为 30.56% , 发热量为 6100大卡 /千克弱粘结性次烟煤送入气载体内热式热解 反应器内进行低温干馏， 干馏气为 660°C乏氧热气体， 经 25min干馏处理后 获得产率为 66.9%, 发热量为 7100大卡 /千克的产品煤， 并回收 8.2%的煤焦 油， 干馏尾气中含尘 140mg/Nm3 (过旋风器后） 。
综上所述， 以上仅为本发明的较佳实施例而已， 并非用于限定本发明 的保护范围， 因此， 凡在本发明的精神和原则之内所作的任何修改、 等同 替换、 改进等， 均应包含在本发明的保护范围之内。

Claims

权 利 要 求 书
1. 一种气载体内热式低阶煤提质工艺， 该工艺包括如下步骤：
1 )经过粉碎和筛分处理的原料煤经过原煤进料溜管加入到反应器底部的 旋转炉蓖中；
2 )乏氧加热气体从设置在反应器下方的热气体进口进入， 并通过炉蓖上 的凿孔与煤样直接接触进行传热， 发生干燥或热解反应；
3 )经过一定反应时间后， 随旋转炉蓖的转动， 处理后的煤样被设置在旋 转炉蓖上方的犁式机械搅拌器刮至卸料口， 热气体尾气经过排气出口排出。
2. 如权利要求 1所述的工艺， 其特征在于， 进入所述反应器的原煤颗粒 粒度分布在 6 ~ 50mm, 进口乏氧加热气体的含氧量小于 1%。
PCT/CN2010/078421 2009-11-06 2010-11-04 一种气载体内热式低阶煤提质工艺 Ceased WO2011054304A1 (zh)

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CN2009102123486A CN101701158B (zh) 2009-11-06 2009-11-06 一种气载体内热式低阶煤提质工艺
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