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WO2012162971A1 - 旋流床粉煤气化方法及其系统 - Google Patents

旋流床粉煤气化方法及其系统 Download PDF

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Publication number
WO2012162971A1
WO2012162971A1 PCT/CN2011/079248 CN2011079248W WO2012162971A1 WO 2012162971 A1 WO2012162971 A1 WO 2012162971A1 CN 2011079248 W CN2011079248 W CN 2011079248W WO 2012162971 A1 WO2012162971 A1 WO 2012162971A1
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Prior art keywords
gas
coal
gasification
cyclone
gasifier
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English (en)
French (fr)
Inventor
吴道洪
王其成
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Beijing Shenwu Environmental and Energy Technology Co Ltd
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Beijing Shenwu Environmental and Energy Technology Co Ltd
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • C10J3/487—Swirling or cyclonic gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/78—High-pressure apparatus
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0909—Drying
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C10J2300/0933—Coal fines for producing water gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C10J2300/0936—Coal fines for producing producer gas

Definitions

  • the present invention relates to a method and system for utilizing coal, and more particularly to a method and system for swirling bed coal gasification. Background technique
  • Coal gasification is one of the most important ways to clean and efficiently use coal. It is the most important unit technology for developing modern coal chemical industry. Coal gasification can produce fuel gas, chemical synthetic feed gas, hydrogen fuel cell, coal-gas combined cycle power generation, and synthetic natural gas.
  • the existing coal gasification technology is divided into: fixed bed gasification technology, fluidized bed gasification technology and entrained flow gasification technology according to the structural characteristics of the coal gasifier and the movement mode of the fuel in the gasification furnace.
  • the fixed bed gasification technology can only use lump coal, can not use the end coal or pulverized coal, the maintenance and operation cost of the equipment is high, and the pressurized fixed bed gasification process also produces harmful substances such as phenols and tar, and gas purification treatment.
  • the process is more complicated and easily causes secondary pollution.
  • a certain amount of carbon must be maintained in the gasifier, and in the fluidized state, the ash is not easily separated from the layer, and the carbon content in the discharged fly ash and ash is higher.
  • the entrained flow gasification technology is divided into wet method (water coal slurry) and dry method according to the feeding method.
  • the equipment and system for wet feeding are single, but because the water used in the pulping process consumes a part of the heat, the carbon conversion rate and gas heat value in coal gasification are lower than that of the dry feed gasifier, and It is suitable for coal with high ash content; the preparation, drying, pressurization and conveying system of coal in dry feeding is complicated, there are many equipments, and the system operation and equipment maintenance cost are expensive. Summary of the invention
  • the invention provides a spinning bed powder coal gasification method and a system thereof with low manufacturing cost, single process cylinder and large raw coal processing capacity.
  • a method for swirling bed coal gasification that achieves one of the objects of the present invention includes the following steps:
  • the preheating temperature of the step (1) is 200-300 ° C, and the total moisture after drying is less than or equal to 8%.
  • the gasification reaction of the step (2) is carried out under the conditions of a pressure of ⁇ 3.0 MPa and a temperature of 900 to 1500 °C.
  • the chilled gas in the step (3) is pressurized by a chilled gas compressor as part of the purified chilled gas, and then sent to a cyclone gasifier for chilling.
  • the water vapor produced by the gas heat exchanger is treated by a high pressure steam boiler and used as a gasification medium together with oxygen produced by the oxygen system.
  • a cyclone powder coal gasification system embodying the second object of the present invention comprising a dry preheater, a cyclone gasifier connected to the dry preheater, connected to the top of the cyclone gasifier a chill gas compressor, a gas heat exchanger connected to a gas outlet of the cyclone gasifier, and a gas purification system connected to a gas outlet of the gas heat exchanger.
  • the purified gas outlet of the gas purification system is branched into a passage connected to the inlet of the chiller compressor.
  • the water vapor outlet of the gas heat exchanger is connected to a high pressure steam boiler, and the water vapor outlet of the high pressure steam boiler is in communication with the oxygen inlet of the swirling bed gasifier.
  • a cyclone dust collector is further disposed between the gas outlet of the cyclone gasifier and the gas heat exchanger.
  • a crusher is arranged at the inlet of the raw material of the dry preheater, and a coal lock bucket and a coal storage bin are arranged in the exit, and an oxygen system is arranged at the oxygen inlet of the cyclone gasification furnace.
  • the cyclone bed coal gasification method and system thereof of the invention have the advantages of a fluidized bed gasification furnace and an entrained flow gasification furnace by using a cyclone bed as a gasification furnace, and the equipment structure is simple, and the manufacturing cost is low.
  • the raw material processing capacity is large and easy to operate.
  • Figure 1 is a schematic view showing the structure of a swirling bed powder coal gasification system of the present invention. detailed description
  • the cyclone powder coal gasification system of the present invention comprises a dry preheater, a cyclone gasifier connected to the dry preheater, and a chill gas compressor connected to the top of the cyclone gasifier, a gas heat exchanger connected to the gas outlet of the cyclone gasifier, and a gas purification system connected to the gas outlet of the gas heat exchanger.
  • the swirling bed powder coal gasification system of the present invention comprises a crusher 1, a dry preheater 2, a coal lock bucket 3, a coal bunker 4 and a cyclone gasifier 6, in turn Connected; the oxygen inlet of the cyclone gasifier 6 is provided with an oxygen system 5, a chill gas compressor 8 connected to the top of the cyclone gasifier 6, and a gas outlet of the cyclone gasifier 6 a connected cyclone 7, a gas heat exchanger 9 connected to the cyclone 7, a gas purification system 11 connected to the gas outlet of the gas heat exchanger 9, and a purified gas outlet of the gas purification system 11
  • the air inlet of the cold air compressor 8 is connected; the water vapor outlet of the gas heat exchanger 9 is connected to a high pressure steam boiler 10, and the water vapor outlet of the high pressure steam boiler 10 is connected to the oxygen inlet of the cyclone gasification furnace 6.
  • the method for swirling bed powder coal gasification of the present invention is as follows:
  • the coal quality analysis of raw coal is shown in Table 1.
  • the raw coal is crushed by the crusher 1 into a particle size of ⁇ 1 mm, and then dried in the dry preheater 2 to a total moisture of 8%, and the temperature after preheating is 250 ° C; after drying and preheating
  • the coal powder passes through the coal lock bucket 3 and the coal-filling silo 4 in turn, and the oxygen from the oxygen-making system 5 and the steam of the high-pressure steam boiler 10 act together to enter the cyclone gasification furnace 6 under pressure, at a pressure of l.
  • Gasification is carried out by gasification reaction at OMPa and temperature of 1000 °C; the produced high-temperature gas is chilled in the upper part of the cyclone gasifier 6, the chill gas is from the chiller compressor 8; the chilled gas is swirled from the vortex
  • the top of the bed gasifier 6 enters the cyclone dust collector 7 to remove dust, and the clean gas enters the gas heat exchanger 9 for further cooling, and then is purified in the gas purification system 11, and a part of the purified gas is pressurized by the chilling gas compressor 8 as chilling gas.
  • the water vapor produced by the gas heat exchanger 9 is treated by the high pressure steam boiler 10 and used together with the oxygen produced by the oxygen generation system 5 as a gasification medium.
  • the gas gas components after purification are shown in Table 2.
  • the coal quality analysis of raw coal is shown in Table 3.
  • the raw coal is crushed by the crusher 1 into a particle size of ⁇ 3 mm, and then dried in the dry preheater 2 to a total moisture of 8%, and the temperature after preheating is 200 ° C; after drying and preheating
  • the coal powder passes through the coal lock bucket 3 and the coal loading bin 4 in turn, and the oxygen from the oxygen system 5 and the steam of the high-pressure steam boiler 10 act together to enter the cyclone gasifier 6 at a pressure of 3.0 MPa.
  • Gasification is carried out by gasification reaction at a temperature of 900 °C; the produced high-temperature gas is chilled in the upper part of the cyclone gasifier 6, the chill gas is from the chiller compressor 8; the chilled gas is from the cyclone bed
  • the top of the gasification furnace 6 enters the cyclone dust collector 7 to remove dust, and the clean gas enters the gas heat exchanger 9 for further cooling, and then is purified in the gas purification system 11, and a part of the purified gas is pressurized by the chilling gas compressor 8 and used as chilling gas.
  • the water vapor produced by the gas heat exchanger 9 is treated by the high pressure steam boiler 10 and used together with the oxygen produced by the oxygen generation system 5 as a gasification medium.
  • the gas gas components after purification are shown in Table 4.
  • the coal quality analysis of raw coal is shown in Table 5.
  • the raw coal is crushed by the crusher 1 into a particle size of ⁇ 3 mm, and then dried in the dry preheater 2 to a total moisture of 8%, and the temperature after preheating is 300 ° C; after drying and preheating
  • the coal powder passes through the coal lock bucket 3 and the coal-filling silo 4 in turn, and the oxygen from the oxygen-making system 5 and the steam of the high-pressure steam boiler 10 act together to enter the cyclone gasification furnace 6 under pressure, at a pressure of l.
  • Gasification is carried out by gasification reaction at OMPa and temperature of 1500 °C; the produced high-temperature gas is chilled in the upper part of the cyclone gasifier 6, the chill gas is from the chiller compressor 8; the chilled gas is swirled from the vortex
  • the top of the bed gasifier 6 enters the cyclone dust collector 7 to remove dust, and the clean gas enters the gas heat exchanger 9 for further cooling, and then is purified in the gas purification system 11, and a part of the purified gas is pressurized by the chilling gas compressor 8 as chilling gas.
  • the water vapor produced by the gas heat exchanger 9 is treated by the high pressure steam boiler 10 and used together with the oxygen produced by the oxygen generation system 5 as a gasification medium.
  • the gas gas components after purification are shown in Table 6.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Abstract

提供了一种旋流床粉煤气化方法及其系统。该方法包括以下步骤：将粒度小于或等于3mm的原料煤在煤干燥预热器（2）内进行干燥和预热；干燥和预热后的原料煤在氧气和水蒸气混合气化剂的共同作用下分上下两路进入旋流床气化炉（6），进行气化反应制备气化煤气；气化煤气在旋流床气化炉（6）顶部激冷后，进入煤气换热器（9）进一步冷却，然后在煤气净化系统（11）进行净化。该系统包括干燥预热器（2）、旋流床气化炉（6）、激冷气压缩机（8）、煤气换热器（9）和煤气净化系统（11）。该旋流床粉煤气化方法和系统具有结构和工艺简单、制造成本低、原煤处理量大的优点。

Description

说 明 书
旋流床粉煤气化方法及其系统
技术领域
本发明涉及一种煤炭利用方法及其系统， 尤其涉及一种旋流床粉煤气化方 法及其系统。 背景技术
进入 21 世纪， 为了减少燃煤对大气的污染， 必须大力发展洁净煤技术。 煤炭气化是洁净、 高效利用煤炭的最主要途径之一， 是发展现代煤化工最重要 的单元技术。 煤炭气化可以生产燃料煤气、 化工合成原料气、 氢燃料电池、 煤 气联合循环发电、 合成天然气等。
现有煤气化技术按照煤气化炉的结构特点和燃料在气化炉中进行转化时 的运动方式分为： 固定床气化技术、 流化床气化技术和气流床气化技术。 其中 固定床气化技术只能用块煤， 不能使用末煤或粉煤， 设备的维护和运行费用较 高， 加压固定床气化工艺还会产生酚类、 焦油等有害物质， 煤气净化处理工艺 较复杂， 易造成二次污染。 在流化床气化工艺中， 气化炉内必须维持一定的含 碳量， 而且在流化状态下灰渣不易从料层分离出来， 排出的飞灰与灰渣中的含 碳量均较高， 热损失较大， 需考虑有效的飞灰回收与循环。 此外， 由于气化温 度的影响， 流化床气化炉的气化强度受到限制， 碳转化率较低， 也不适合于气 化粘结性强的煤。 气流床气化技术根据进料方式分为湿法 （水煤浆） 和干法 两种。 湿法进料的设备及系统筒单， 但由于制浆过程中掺人的水要消耗一部分 热量， 煤气化中的碳转化率和煤气热值低于干法进料的气化炉， 而且不适用含 灰多的煤种； 干法进料中煤的制备、 干燥、 加压及输送系统复杂， 设备较多， 系统运行和设备维护费用昂贵。 发明内容
本发明提供了一种制造成本低， 工艺筒单， 原煤处理量大的旋流床粉煤气 化方法及其系统。 实现本发明的目的之一的旋流床粉煤气化方法， 包括如下步骤：
( 1 )将粒度小于或等于 3mm的原料煤在干燥预热器内进行干燥和预热； ( 2 )干燥和预热后的原料煤在氧气和水蒸汽混合气化剂的共同作用下分 上下两路进入旋流床气化炉， 进行气化反应制备气化煤气；
( 3 )气化煤气在旋流床气化炉顶部激冷后， 进入煤气换热器进一步冷却， 然后在煤气净化系统进行净化。
所述步骤（ 1 ) 的预热温度为 200-300°C , 干燥后全水分小于或等于 8%。 所述步骤（2 ) 的气化反应在压力≤3.0MPa, 温度 900- 1500 °C条件下进行。 所述步骤（3 ) 中的激冷气为净化后的煤气的一部分经激冷气压缩机增压 后送入旋流床气化炉进行激冷。
所述煤气换热器生产的水蒸气经高压蒸汽锅炉处理后， 与制氧系统生产的 氧气一起作为气化介质使用。
实现本发明的目的之二的旋流床粉煤气化系统， 包括干燥预热器， 与所述 干燥预热器相连的旋流床气化炉， 与所述旋流床气化炉顶部相连的激冷气压缩 机， 与所述旋流床气化炉的煤气出口相连的煤气换热器， 与所述煤气换热器的 煤气出口相连的煤气净化系统。
所述煤气净化系统的净化煤气出口分出一个通道与所述激冷气压缩机的 进气口相连。
所述煤气换热器的水蒸气出口连接有高压蒸汽锅炉， 所述高压蒸汽锅炉的 水蒸气出口与所述旋流床气化炉的氧气入口相通。
所述旋流床气化炉的煤气出口与所述煤气换热器之间还设有旋风除尘器。 所述干燥预热器的原料进口处设有破碎机， 出口处依次设有煤锁斗和加煤 仓， 所述旋流床气化炉的氧气进口处设有制氧系统。
本发明的旋流床粉煤气化方法及其系统， 由于采用旋流床作为气化炉， 集 成了流化床气化炉和气流床气化炉的优点， 设备结构筒单、 制造成本低， 原料 处理量大， 易操作。 附图说明
图 1为本发明的旋流床粉煤气化系统的结构示意图。 具体实施方式
下面结合附图更详细地说明本发明。
本发明的旋流床粉煤气化系统， 包括干燥预热器， 与所述干燥预热器相连 的旋流床气化炉， 与所述旋流床气化炉顶部相连的激冷气压缩机， 与所述旋流 床气化炉的煤气出口相连的煤气换热器， 与所述煤气换热器的煤气出口相连的 煤气净化系统。
具体地， 如图 1所示， 本发明的旋流床粉煤气化系统， 包括破碎机 1 , 干 燥预热器 2, 煤锁斗 3 , 加煤仓 4和旋流床气化炉 6, 依次相连； 旋流床气化炉 6的氧气进口处设有制氧系统 5,与旋流床气化炉 6顶部相连的激冷气压缩机 8, 与所述旋流床气化炉 6的煤气出口相连的旋风除尘器 7, 与旋风除尘器 7相连 的煤气换热器 9, 与煤气换热器 9的煤气出口相连的煤气净化系统 11 ; 煤气净 化系统 11的净化煤气出口分出一个通道与激冷气压缩机 8的进气口相连； 煤 气换热器 9的水蒸气出口连接有高压蒸汽锅炉 10, 高压蒸汽锅炉 10的水蒸气 出口与旋流床气化炉 6的氧气入口相通。
本发明的旋流床粉煤气化方法实施例如下：
实施例 1
以煤处理量 2t/h的生产规模为例，原料煤的煤质分析见表 1。如图 1所示， 原料煤经破碎机 1破碎成≤lmm的粒径， 然后在干燥预热器 2内干燥到全水分 8%,预热后温度为 250°C ;干燥和预热后的煤粉依次通过煤锁斗 3和加煤仓 4, 经来自制氧系统 5的氧气和高压蒸汽锅炉 10的水蒸气共同作用下分上下两路 进入旋流床气化炉 6, 在压力 l.OMPa和温度 1000 °C条件下进行气化反应制备 煤气； 生产的高温煤气在旋流床气化炉 6上部进行激冷， 激冷气来自于激冷气 压缩机 8; 激冷后的煤气从旋流床气化炉 6顶部进入旋风除尘器 7除尘， 洁净 的煤气进入煤气换热器 9进一步冷却， 然后在煤气净化系统 11进行净化， 其 中一部分净化煤气经激冷气压缩机 8增压后作为激冷气使用； 煤气换热器 9生 产的水蒸气经高压蒸汽锅炉 10处理后， 与制氧系统 5生产的氧气一起作为气 化介质使用。 净化后的煤气气体组分见表 2
表 1 原料煤的煤质分析结果（％ )
Figure imgf000006_0001
表 2 煤气的气体组
Figure imgf000006_0002
实施例 2
以煤处理量 2t/h的生产规模为例，原料煤的煤质分析见表 3。如图 1所示， 原料煤经破碎机 1破碎成≤3mm的粒径， 然后在干燥预热器 2内干燥到全水分 8% ,预热后温度为 200°C ;干燥和预热后的煤粉依次通过煤锁斗 3和加煤仓 4, 经来自制氧系统 5的氧气和高压蒸汽锅炉 10的水蒸气共同作用下分上下两路 进入旋流床气化炉 6 ,在压力 3.0MPa和温度 900 °C条件下进行气化反应制备煤 气； 生产的高温煤气在旋流床气化炉 6上部进行激冷， 激冷气来自于激冷气压 缩机 8; 激冷后的煤气从旋流床气化炉 6顶部进入旋风除尘器 7除尘， 洁净的 煤气进入煤气换热器 9进一步冷却， 然后在煤气净化系统 11进行净化， 其中 一部分净化煤气经激冷气压缩机 8增压后作为激冷气使用； 煤气换热器 9生产 的水蒸气经高压蒸汽锅炉 10处理后， 与制氧系统 5生产的氧气一起作为气化 介质使用。 净化后的煤气气体组分见表 4
表 3 原料煤的煤质分析结果（％)
Figure imgf000007_0001
表 4 煤气的气体组
Figure imgf000007_0002
实施例 3
以煤处理量 2t/h的生产规模为例，原料煤的煤质分析见表 5。如图 1所示， 原料煤经破碎机 1破碎成≤3mm的粒径， 然后在干燥预热器 2内干燥到全水分 8%,预热后温度为 300°C ;干燥和预热后的煤粉依次通过煤锁斗 3和加煤仓 4, 经来自制氧系统 5的氧气和高压蒸汽锅炉 10的水蒸气共同作用下分上下两路 进入旋流床气化炉 6, 在压力 l.OMPa和温度 1500 °C条件下进行气化反应制备 煤气； 生产的高温煤气在旋流床气化炉 6上部进行激冷， 激冷气来自于激冷气 压缩机 8; 激冷后的煤气从旋流床气化炉 6顶部进入旋风除尘器 7除尘， 洁净 的煤气进入煤气换热器 9进一步冷却， 然后在煤气净化系统 11进行净化， 其 中一部分净化煤气经激冷气压缩机 8增压后作为激冷气使用； 煤气换热器 9生 产的水蒸气经高压蒸汽锅炉 10处理后， 与制氧系统 5生产的氧气一起作为气 化介质使用。 净化后的煤气气体组分见表 6
表 5 原料煤的煤质分析结果（％)
Figure imgf000008_0001
表 6 煤气的气体组
Figure imgf000008_0002

Claims

权 利 要 求 书
1、 一种旋流床粉煤气化方法， 包括如下步骤：
( 1 )将粒度小于或等于 3mm的原料煤在干燥预热器内进行干燥和预热； ( 2 )干燥和预热后的原料煤在氧气和水蒸汽混合气化剂的共同作用下分 上下两路进入旋流床气化炉， 进行气化反应制备气化煤气；
( 3 )气化煤气在旋流床气化炉顶部激冷后， 进入煤气换热器进一步冷却， 然后在煤气净化系统进行净化。
2、 根据权利要求 1 所述的旋流床粉煤气化方法， 其特征在于： 所述步骤
( 1 ) 的预热温度为 200-300°C , 干燥后全水分小于或等于 8%。
3、 根据权利要求 1 所述的旋流床粉煤气化方法， 其特征在于： 所述步骤
( 2 ) 的气化反应在压力≤3.0MPa, 温度 900- 1500 °C条件下进行。
4、 根据权利要求 1 所述的旋流床粉煤气化方法， 其特征在于： 所述步骤
( 3 ) 中的激冷气为净化后的煤气的一部分经激冷气压缩机增压后送入旋流床 气化炉进行激冷。
5、 根据权利要求 1 所述的旋流床粉煤气化方法， 其特征在于： 所述煤气 换热器生产的水蒸气经高压蒸汽锅炉处理后， 与制氧系统生产的氧气一起作为 气化介质使用。
6、 一种旋流床粉煤气化系统， 包括： 干燥预热器， 与所述干燥预热器相 连的旋流床气化炉， 与所述旋流床气化炉顶部相连的激冷气压缩机， 与所述旋 流床气化炉的煤气出口相连的煤气换热器， 与所述煤气换热器的煤气出口相连 的煤气净化系统。
7、 根据权利要求 6所述的旋流床粉煤气化系统， 其特征在于： 所述煤气 净化系统的净化煤气出口分出一个通道与所述激冷气压缩机的进气口相连。
8、 根据权利要求 6所述的旋流床粉煤气化系统， 其特征在于： 所述旋流 床气化炉的煤气出口与所述煤气换热器之间还设有旋风除尘器。
9、 根据权利要求 6所述的旋流床粉煤气化系统， 其特征在于： 所述干燥 预热器的原料进口处设有破碎机， 出口处依次设有煤锁斗和加煤仓， 所述旋流 床气化炉的氧气进口处设有制氧系统。
10、 根据权利要求 6所述的旋流床粉煤气化系统， 其特征在于： 所述煤气 换热器的水蒸气出口连接有高压蒸汽锅炉， 所述高压蒸汽锅炉的水蒸气出口与 所述旋流床气化炉的氧气入口相通。
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