CN1597871A - Technical process for gasification of fluidized-bed CO gasifying furnace and apparatus thereof - Google Patents
Technical process for gasification of fluidized-bed CO gasifying furnace and apparatus thereof Download PDFInfo
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- 238000002309 gasification Methods 0.000 title claims abstract description 93
- 238000000034 method Methods 0.000 title claims abstract description 40
- 230000008569 process Effects 0.000 title claims abstract description 19
- 239000003245 coal Substances 0.000 claims abstract description 48
- 239000002994 raw material Substances 0.000 claims abstract description 22
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 15
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000003830 anthracite Substances 0.000 claims abstract description 8
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 4
- 239000003077 lignite Substances 0.000 claims abstract description 3
- 239000007789 gas Substances 0.000 claims description 68
- 238000002485 combustion reaction Methods 0.000 claims description 20
- 238000000746 purification Methods 0.000 claims description 20
- 238000006243 chemical reaction Methods 0.000 claims description 17
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 14
- 239000003546 flue gas Substances 0.000 claims description 14
- 238000002844 melting Methods 0.000 claims description 10
- 230000008018 melting Effects 0.000 claims description 10
- 229910052799 carbon Inorganic materials 0.000 claims description 9
- 239000000428 dust Substances 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 239000000571 coke Substances 0.000 claims description 6
- 238000005243 fluidization Methods 0.000 claims description 5
- 229910000831 Steel Inorganic materials 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 230000000694 effects Effects 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 34
- 229910002092 carbon dioxide Inorganic materials 0.000 description 17
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 239000002956 ash Substances 0.000 description 6
- 238000001816 cooling Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
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- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 239000003476 subbituminous coal Substances 0.000 description 2
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
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- 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
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
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Abstract
本发明涉及煤化工领域的煤气化新工艺,为一种用O2+CO2或空气+CO2为气化剂的流化床CO气化炉的气化工艺方法及其装置。其以O2和CO2为气化剂,0~10mm焦粉、无烟煤为原料,采用连续气化工作的流化床气化炉为气化设备,即连续气化法或以空气和CO2为气化剂,0~10mm焦粉、无烟煤、贫煤、长焰煤、褐煤为原料,采用间歇气化工作的流化床气化炉为气化设备,即间歇气化法,使CO2气还原成CO气,制取高纯度CO气,用作有机合成原料。其优点在于原料来源丰富,回收利用CO2作为气化剂,不仅可产生经济效益,而且可以改善环境状况,以流化床气化炉为气化设备,反应速度快,易达到平衡组分,获得高组分的CO气。
The invention relates to a new coal gasification process in the field of coal chemical industry, and relates to a gasification process and a device for a fluidized bed CO gasifier using O2 + CO2 or air+ CO2 as a gasification agent. It uses O 2 and CO 2 as gasification agents, 0-10mm coke powder and anthracite as raw materials, and adopts fluidized bed gasification furnace for continuous gasification as gasification equipment, that is, continuous gasification method or air and CO 2 As a gasification agent, 0-10mm coke powder, anthracite, lean coal, long-flame coal, and lignite are used as raw materials, and a fluidized bed gasifier with intermittent gasification work is used as gasification equipment, that is, intermittent gasification method, to make CO 2 The gas is reduced to CO gas to produce high-purity CO gas, which is used as a raw material for organic synthesis. Its advantage is that the source of raw materials is abundant, and recycling CO2 as a gasification agent can not only generate economic benefits, but also improve the environmental conditions. The fluidized bed gasifier is used as the gasification equipment, and the reaction speed is fast, and it is easy to reach the equilibrium composition. Obtain high-component CO gas.
Description
所属技术领域Technical field
本发明涉及煤化工领域的煤气化新工艺,特指一种流化床CO气化炉的气化工艺方法及其装置。The invention relates to a new coal gasification process in the field of coal chemical industry, in particular to a gasification process method and a device for a fluidized bed CO gasifier.
背景技术Background technique
CO是一碳化学的主要有机合成原料,它与水、甲醇、氨等反应生成甲酸、甲酰胺、醋酸等有机化学品。目前国内生产CO气多采用固定床气化炉,生产水煤气或空气煤气,然后再从水煤气或空气煤气中分离得到高纯度的CO气。我国有采用CO和甲醇工艺生产醋酸的企业,用CO2和O2为气化剂,用固定床气化炉生产CO气,这种工艺由于采用铸造焦为原料,原料价格高,由于固定床气化炉沿炉高度的温度是逐渐下降的,在炉出口温度约为600℃,由于
发明内容Contents of the invention
本发明的目的是针对现有技术的缺陷,提出一种用O2+CO2或空气+CO2为气化剂的流化床CO气化炉的气化工艺方法及其装置。The object of the present invention is to address the defects of the prior art and propose a gasification process and device for a fluidized bed CO gasifier using O 2 +CO 2 or air + CO 2 as the gasification agent.
实现上述目的的技术方案为采用流化床气化炉为主要设备,以含氧气体和CO2为气化剂,以粉焦或粉煤为原料,通过流化床气化炉进行碳的气化反应,采用连续气化法或间歇气化法,使CO2气还原成CO气,制取高纯度CO气,用作有机合成原料。The technical solution to achieve the above purpose is to use a fluidized bed gasifier as the main equipment, use oxygen-containing gas and CO2 as the gasification agent, and use powdered coke or pulverized coal as raw materials to gasify carbon through the fluidized bed gasifier. Chemical reaction, using continuous gasification method or batch gasification method, reducing CO2 gas to CO gas, producing high-purity CO gas, which can be used as a raw material for organic synthesis.
所述的连续气化法是以O2和CO2为气化剂,0~10mm焦粉、无烟煤为原料,采用连续气化工作的流化床气化炉为气化设备,并根据原料煤的灰熔点,确定流化床气化炉的工作温度,低于灰熔点150℃~250℃,流化床气化炉的流化速度为0.8m~1.2m/s,生成的CO气经高温旋风分离器除尘、分离下的含碳粉尘经下料管、返料器返入炉内重新参与反应,初除尘的CO气再经管式换热器与入炉的CO2气体换热后,进入煤气净化系统,进一步洗涤、除尘后送往气柜待加工。The continuous gasification method uses O2 and CO2 as gasification agents, 0-10mm coke powder and anthracite as raw materials, and adopts a fluidized bed gasifier for continuous gasification work as gasification equipment, and according to the raw material coal The ash melting point of the fluidized bed gasifier determines the working temperature of the fluidized bed gasifier, which is 150°C to 250°C lower than the ash melting point, and the fluidization velocity of the fluidized bed gasifier is 0.8m to 1.2m/s. The cyclone separator removes dust, and the separated carbon-containing dust is returned to the furnace through the feeding pipe and the feeder to participate in the reaction again. After entering the gas purification system, further washing and dust removal, it is sent to the gas cabinet for processing.
所述的间歇气化法是以空气和CO2为气化剂,0~10mm焦粉、无烟煤、贫煤、长焰煤、褐煤为原料,采用间歇气化工作的流化床气化炉为气化设备,生产CO气;整个制气过程分供空气燃烧和供CO2气化两个阶段,燃烧阶段与气化阶段的时间分配约为4∶6,两阶段循环交替,流化床气化炉的最高工作温度,低于原料煤的灰熔点150℃~250℃,一般转换温度范围为50℃→100℃,流化床气化炉的流化速度0.8~1.2m/s。The intermittent gasification method uses air and CO as gasification agents, 0-10mm coke powder, anthracite, lean coal, long-flame coal, and lignite as raw materials, and adopts a fluidized bed gasifier for intermittent gasification. Gasification equipment, producing CO gas; the whole gas production process is divided into two stages: air combustion and CO2 gasification, the time distribution between the combustion stage and the gasification stage is about 4:6, the two stages cycle alternately, and the fluidized bed gas The maximum working temperature of the gasifier is 150°C to 250°C lower than the ash melting point of raw coal, the general conversion temperature range is 50°C→100°C, and the fluidization velocity of the fluidized bed gasifier is 0.8 to 1.2m/s.
供空气燃烧阶段,向气化炉供入空气,使炉内的煤料在流化状态下燃烧,床层温度迅速升高,当床层温度升到预定最高工作温度时,停止供风;气化炉转入供CO2气的气化阶段,向气化炉供入CO2气,使炉内的高温料层在流化状态下进行布杜阿尔反应,生成CO气。由于该反应是强吸热反应,床层温度迅速下降,当床层温度下降到预定温度时(视原料煤的活性而定,一般大于950℃),停止供入CO2气。In the air supply combustion stage, air is supplied to the gasifier to make the coal in the furnace burn in a fluidized state, and the bed temperature rises rapidly. When the bed temperature rises to the predetermined maximum working temperature, the air supply is stopped; The gasification furnace is transferred to the gasification stage of supplying CO 2 gas, and CO 2 gas is supplied to the gasification furnace, so that the high-temperature material layer in the furnace undergoes a Boudual reaction in a fluidized state to generate CO gas. Since the reaction is a strong endothermic reaction, the bed temperature drops rapidly. When the bed temperature drops to a predetermined temperature (depending on the activity of the raw coal, generally greater than 950°C), the supply of CO2 gas is stopped.
当以水分和挥发分高的煤种为原料时,采取在燃烧阶段加煤,使煤在燃烧阶段除掉水分、挥发分而成为焦碳。When coal with high moisture and volatile content is used as raw material, coal is added during the combustion stage, so that the coal can remove moisture and volatile content during the combustion stage and become coke.
实施连续气化法的装置包括循环流化床气化炉(1)、旋风分离器(2)、下料管(4)、返料器(5)、管式换热器(3)、CO净化系统(10),其中流化床气化炉(1)上部为园筒形,下部为倒锥形,炉体为耐火衬里的钢板结构,炉体下部顺序设有风室(7)、排渣阀,煤仓(8)经螺旋加煤机(9)与气化炉(1)相连;炉体上部炉出口上设有旋风分离器(2),旋风分离器(2)下端顺序连接下料管(4)、返料器(5),经返料器(5)与流化床气化炉(1)相连,旋风分离器(2)的顶端出口与管式换热器(3)相连,其下端烟气出口与CO净化系统(10)相连,换热气体出口与文丘里混合器(6)相连。The device for implementing the continuous gasification method includes a circulating fluidized bed gasifier (1), a cyclone separator (2), a feeding pipe (4), a feeder (5), a tubular heat exchanger (3), a CO Purification system (10), wherein the upper part of the fluidized bed gasification furnace (1) is cylindrical, the lower part is inverted conical, the furnace body is a steel plate structure with refractory lining, and the lower part of the furnace body is sequentially provided with air chamber (7), exhaust The slag valve and the coal bin (8) are connected to the gasifier (1) through the spiral coal stoker (9); the upper part of the furnace body is equipped with a cyclone separator (2) at the outlet of the furnace, and the lower end of the cyclone separator (2) is sequentially connected to the lower The material pipe (4), the feeder (5), is connected to the fluidized bed gasifier (1) through the feeder (5), and the top outlet of the cyclone separator (2) is connected to the tubular heat exchanger (3) The flue gas outlet at the lower end is connected with the CO purification system (10), and the heat exchange gas outlet is connected with the Venturi mixer (6).
实施间歇气化法的装置包括间歇式流化床气化炉(1)、旋风分离器(2)、下料管(4)、返料器(5)、管式换热器(3)、CO净化系统(10)、烟气净化系统(13),其中流化床气化炉(1)上部为园筒形,下部为倒锥形,炉体为耐火衬里的钢板结构,炉体下部顺序设有风室(7)、排渣阀,煤仓(8)经螺旋加煤机(9)与气化炉(1)相连;炉体上部炉出口上顺序设有旋风分离器(2),旋风分离器(2)下端顺序连接下料管(4)、返料器(5),经返料器(5)与流化床气化炉(1)相连,旋风分离器(2)的顶端出口与管式换热器(3)相连,在管式换热器(3)上端设有与CO2换向阀(11-1)、空气换向阀(11-2)分别相连的气体进口,下端出口经CO换向阀(12-1)、烟气换向阀(12-2)分别与CO净化系统(10)、烟气净化系统(13)相连,下端并设有与风室(7)的进气口相连的换热气体出口。The device for implementing the batch gasification method includes a batch fluidized bed gasifier (1), a cyclone separator (2), a feeding pipe (4), a feeder (5), a tubular heat exchanger (3), CO purification system (10) and flue gas purification system (13), wherein the upper part of the fluidized bed gasification furnace (1) is cylindrical, the lower part is inverted conical, the furnace body is a steel plate structure with refractory lining, and the lower part of the furnace body is sequentially An air chamber (7) and a slag discharge valve are provided, and the coal bunker (8) is connected to the gasifier (1) through a spiral stoker (9); the upper part of the furnace body is equipped with a cyclone separator (2) sequentially on the outlet of the furnace, The lower end of the cyclone separator (2) is sequentially connected with the feeding pipe (4) and the feeder (5), and connected with the fluidized bed gasification furnace (1) through the feeder (5), and the top of the cyclone separator (2) The outlet is connected to the tubular heat exchanger (3), and the upper end of the tubular heat exchanger (3) is provided with a gas inlet respectively connected to the CO2 reversing valve (11-1) and the air reversing valve (11-2) , the outlet at the lower end is connected to the CO purification system (10) and the flue gas purification system (13) respectively via the CO reversing valve (12-1) and the flue gas reversing valve (12-2), and the lower end is also provided with an air chamber ( 7) The air inlet connected to the heat exchange gas outlet.
本发明较现有采用固定床CO气化炉的方法具有下述优点:The present invention has the following advantages compared with the existing method using a fixed-bed CO gasifier:
(1)原料来源丰富。流化床连续气化,可使用0~10mm的焦粉及无烟煤粉;而流化床间歇气化法,不仅可使用0~10mm的焦粉、无烟煤粉,而且可使用0~10mm的贫煤、次烟煤及长焰煤等。(1) Abundant sources of raw materials. Fluidized bed continuous gasification can use 0-10mm coke powder and anthracite coal powder; while fluidized bed intermittent gasification can not only use 0-10mm coke powder and anthracite powder, but also 0-10mm lean coal , sub-bituminous coal and long-flame coal, etc.
(2)将CO2作为气化剂,由于CO2是温室效应气体,它的回收利用,不仅可产生经济效益,而且可以改善环境状况。(2) CO 2 is used as a gasification agent. Since CO 2 is a greenhouse gas, its recycling can not only generate economic benefits, but also improve the environment.
(3)由于流化床气化炉在流化状况下与CO2进行充分接触反应,在相同温度下,反应速度快,易达到平衡组分。由于炉内料层温度均匀,容易达到高组分的CO气。(3) Since the fluidized bed gasifier fully contacts and reacts with CO 2 under the condition of fluidization, at the same temperature, the reaction speed is fast and it is easy to reach the equilibrium composition. Due to the uniform temperature of the material layer in the furnace, it is easy to achieve high-component CO gas.
附图说明Description of drawings
图1是本发明连续气化工艺流程图。Figure 1 is a flow chart of the continuous gasification process of the present invention.
图2是本发明流化床间歇气化工艺流程图。Fig. 2 is a flow chart of the fluidized bed batch gasification process of the present invention.
1流化床气化炉 2旋风分离器 3管式换热器 4下料管 5返料器 6文丘里混合器 7风室 8煤仓 9螺旋加煤机 10 CO净化系统 11-1 CO2换向阀11-2空气换向阀 12-1 CO换向阀 12-2烟气换向阀 13烟气净化系统1 Fluidized
具体实施方式Detailed ways
1.流化床连续气化法1. Fluidized bed continuous gasification method
如图1所示,该工艺是以纯氧(≥98%)与CO2气体混合为气化剂,0~10mm的焦粉为原料经螺旋加煤机(9)送入气化炉(1)内,CO2气经管式换热器(3)加热至600℃后,再经文丘里混合器(6)按比例与氧混合后,由风室(7)进入气化炉(1),使炉内的碳层在流化状态与O2和CO2在高温下进行氧化还原反应,生成CO气,由于该反应是发热与吸热反应,床层温度应下降,当两反应处于热量平衡时,床层温度处于稳定状态。该温度根据煤焦的灰熔点而定,一般不超过1150℃。生成的高温CO气由气化炉(1)出口经旋风分离器(2),分离下的含碳粉尘经下料管(4)返料器(5)返入气化炉(1)内重新参与反应。除尘后的CO气进入管式换热器(3)与进入系统的CO2原料气换热。经管式换热器(3)换热器的粗CO气再送入净化系统(10)经进一步洗涤除尘冷却后再送往煤气柜待加工。As shown in Figure 1, this process uses pure oxygen (≥98%) mixed with CO2 gas as a gasification agent, and coke powder with a thickness of 0-10mm is used as a raw material to be sent to the gasifier (1) through a spiral stoker (9). Inside, the CO 2 gas is heated to 600°C by the tubular heat exchanger (3), then mixed with oxygen in proportion by the Venturi mixer (6), and then enters the gasifier (1) from the air chamber (7), so that The carbon layer in the furnace undergoes a redox reaction with O2 and CO2 at high temperature in a fluidized state to generate CO gas. Since this reaction is an exothermic and endothermic reaction, the bed temperature should drop. When the two reactions are in thermal equilibrium , the bed temperature is in a steady state. The temperature depends on the ash melting point of coal char, and generally does not exceed 1150°C. The generated high-temperature CO gas is passed through the cyclone separator (2) from the outlet of the gasifier (1), and the separated carbon-containing dust is returned to the gasifier (1) through the feeding pipe (4) and the feeder (5) Re-engage the response. The CO gas after dedusting enters the tubular heat exchanger (3) to exchange heat with the CO2 feed gas entering the system. The crude CO gas passed through the tubular heat exchanger (3) is sent to the purification system (10) and then sent to the gas cabinet for processing after further washing, dedusting and cooling.
2.流化床间歇气化法2. Fluidized bed batch gasification method
如图2所示,该工艺是以空气和CO2为气化剂。流化床气化炉采用间歇工作法,即整个制气过程分为二个阶段:供空气燃烧阶段,向气化炉供入空气,使炉内的煤料在流化状态下燃烧,床层温度迅速升高当床层温度升到预定温度时(视原料煤的灰熔点而定,一般低于灰熔点温度150℃~250℃),停止供风;气化炉转入供CO2气的气化阶段,向气化炉供入CO2气,使炉内的高温料层在流化状态下进行布杜阿尔反应,生成CO气。由于该反应是强吸热反应,床层温度迅速下降,当床层温度下降到预定温度时(视原料煤的活性而定,一般大于950℃),停止供入CO2气。气化炉又转入供风燃烧阶段。这样两个阶段交替往复,制取CO气。因整个过程都在流化状态下进行的,混合均匀床层温度也非常均匀,反应非常迅速。无需固定床气化炉的其他阶段,操作简单,易于自动化。As shown in Figure 2, the process uses air and CO2 as gasification agents. The fluidized bed gasification furnace adopts the intermittent working method, that is, the whole gas production process is divided into two stages: the air supply combustion stage, supplying air to the gasification furnace to make the coal in the furnace burn in a fluidized state, and the bed layer The temperature rises rapidly. When the bed temperature rises to the predetermined temperature (depending on the ash melting point of the raw coal, generally 150°C-250°C lower than the ash melting point), the air supply is stopped; the gasifier is switched to CO2 gas supply. In the gasification stage, CO 2 gas is supplied to the gasification furnace, so that the high-temperature material layer in the furnace undergoes a Boudouard reaction in a fluidized state to generate CO gas. Since the reaction is a strong endothermic reaction, the bed temperature drops rapidly. When the bed temperature drops to a predetermined temperature (depending on the activity of the raw coal, generally greater than 950°C), the supply of CO2 gas is stopped. The gasification furnace is transferred to the air supply combustion stage. These two stages reciprocate alternately to produce CO gas. Because the whole process is carried out in a fluidized state, the temperature of the mixed bed is also very uniform, and the reaction is very rapid. No other stages of fixed bed gasifier are required, the operation is simple and easy to automate.
其具体实施步骤为0~10mm的原料煤,从煤仓(8)由螺旋加煤机(9)加入炉内。在供空气燃烧阶段。由罗茨风机来的空气依次经空气换向阀11-2,管式换热器(3),空气被加热到600℃后,经风室(7)进入气化炉(1)内,使炉内的料层在流化状态下燃烧,床层温度迅速升高,当床层温度升到1100℃时,停止供入空气,气化炉转入供CO2气的气化阶段。这时空气换向阀11-2关闭,烟气换向阀12-2关闭,CO2换向阀11-1和CO换向阀12-1开启,向气化炉(1)供入CO2气,依次经CO2换向阀11-1,管式换热器(3)、CO2被加热到600℃经风室(7)进入气化炉(1)内,与高温料层在流化状态下进行布杜阿尔反应,生成CO气。床层温度开始下降,温度下降到950℃时,停止供入CO2气。气化炉又转入供空气燃烧阶段。在燃烧阶段产生的高温烟气从炉出口进入旋风分离器(2),分离下的含碳粉尘经下料管(4)返料器(5),返入气化炉(1)重新燃烧。初除尘的高温烟气经管式换热器(3),换热降温到500℃以下,经烟气换热阀12-2进入烟气净化系统(13)。进一步降温降尘,含尘达到排放标准后排入大气。在气化阶段产生的CO气,从炉出口进入旋风分离器(2),分离下的含碳粉尘经下料管(4),返料器(5),返入炉内重新气化,初除尘的CO气经管式换热器(3)换热降温到500℃以下,经CO气换向阀12-1进入CO净化系统(10)冷却除尘,降温后送入CO气柜待加工。供空气燃烧阶段和供二氧化碳气化阶段的转换,根据设定的温度自动进行。The specific implementation steps are that the raw coal of 0-10 mm is fed into the furnace from the coal bunker (8) by the spiral coal stoker (9). In the air supply combustion stage. The air from the Roots blower passes through the air reversing valve 11-2 and the tube heat exchanger (3) successively. After the air is heated to 600°C, it enters the gasifier (1) through the air chamber (7), so that The material bed in the furnace burns in a fluidized state, and the bed temperature rises rapidly. When the bed temperature rises to 1100°C, the air supply is stopped, and the gasifier enters the CO 2 gasification stage. At this time, the air reversing valve 11-2 is closed, the flue gas reversing valve 12-2 is closed, the CO2 reversing valve 11-1 and the CO reversing valve 12-1 are opened, and CO2 is supplied to the gasifier (1) The gas passes through the CO 2 reversing valve 11-1 in turn, the tubular heat exchanger (3), and the CO 2 is heated to 600°C and enters the gasifier (1) through the air chamber (7), where it flows with the high-temperature material layer. The Boudouard reaction is carried out in the reduced state to generate CO gas. The bed temperature began to drop, and when the temperature dropped to 950°C, the supply of CO 2 gas was stopped. The gasification furnace is transferred to the stage of supplying air for combustion. The high-temperature flue gas generated during the combustion stage enters the cyclone separator (2) from the furnace outlet, and the separated carbon-containing dust passes through the feeding pipe (4) and the return device (5), and returns to the gasifier (1) for re-combustion . The high-temperature flue gas from the initial dedusting passes through the tubular heat exchanger (3), heat exchange and cools down to below 500°C, and enters the flue gas purification system (13) through the flue gas heat exchange valve 12-2. Further cooling and dust reduction, after the dust reaches the emission standard, it is discharged into the atmosphere. The CO gas produced in the gasification stage enters the cyclone separator (2) from the furnace outlet, and the separated carbon-containing dust passes through the feeding pipe (4) and the return device (5), and returns to the furnace for re-gasification. The initially dedusted CO gas is cooled to below 500°C through the tubular heat exchanger (3), and enters the CO purification system (10) through the CO gas reversing valve 12-1 for cooling and dedusting. The transition between the combustion stage for air and the gasification stage for carbon dioxide is automatically carried out according to the set temperature.
该制气过程的一个循环为4~5分钟,供空气燃烧阶段的为循环时间40%,供CO2制气阶段约为循环时间60%。流化床间歇气化法由于不需要制氧设备,投资小,运行成本低,适用于中小气源工程,流化床间歇式气化法,原料来源广,几乎所有煤种均适用。特别是次烟煤,长焰煤等挥发高的年青煤种。这些煤灰熔点低,活性好,挥发分和水分高。用于连续气化时,产品气中H2和碳氮化合物的含量高。为以后CO的提纯造成困难。而在间歇气化时在供空气燃烧阶段加煤,入炉煤水分和挥发分在燃烧阶段被迅速干燥干馏而燃烧;到供CO2气化阶段,原料煤已成为焦碳。因此,煤中的水分、挥发分已不对产品气产生影响,这也是该气化法一大优点。One cycle of the gas production process is 4 to 5 minutes, the air supply combustion stage is 40% of the cycle time, and the CO2 gas production stage is about 60% of the cycle time. The fluidized bed batch gasification method does not require oxygen production equipment, has small investment and low operating costs, and is suitable for small and medium gas source projects. The fluidized bed batch gasification method has a wide range of raw material sources and is applicable to almost all types of coal. Especially sub-bituminous coal, long-flame coal and other young coals with high volatility. These coal ash have low melting point, good activity, high volatile matter and moisture content. When used in continuous gasification, the content of H2 and carbon nitrogen compounds in the product gas is high. It will cause difficulties for the purification of CO in the future. In the intermittent gasification, coal is added in the air supply combustion stage, and the moisture and volatile matter of the incoming coal are quickly dried and dry-distilled and burned in the combustion stage; in the CO 2 gasification stage, the raw coal has become coke. Therefore, the moisture and volatile matter in the coal no longer affect the product gas, which is also a major advantage of this gasification method.
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