CN114032392B - Method for preparing aluminum silicon powder from high-aluminum coal - Google Patents
Method for preparing aluminum silicon powder from high-aluminum coal Download PDFInfo
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- 239000003245 coal Substances 0.000 title claims abstract description 94
- CSDREXVUYHZDNP-UHFFFAOYSA-N alumanylidynesilicon Chemical compound [Al].[Si] CSDREXVUYHZDNP-UHFFFAOYSA-N 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title claims abstract description 25
- 229910052782 aluminium Inorganic materials 0.000 title description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 90
- 239000002002 slurry Substances 0.000 claims abstract description 87
- 238000005262 decarbonization Methods 0.000 claims abstract description 72
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 57
- 239000003546 flue gas Substances 0.000 claims abstract description 57
- 238000006243 chemical reaction Methods 0.000 claims abstract description 42
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000000428 dust Substances 0.000 claims abstract description 25
- 238000011084 recovery Methods 0.000 claims abstract description 19
- 239000011863 silicon-based powder Substances 0.000 claims abstract description 19
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 11
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 11
- 238000005261 decarburization Methods 0.000 claims description 51
- 239000002245 particle Substances 0.000 claims description 24
- 238000003860 storage Methods 0.000 claims description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 15
- 239000010419 fine particle Substances 0.000 claims description 15
- 229910052760 oxygen Inorganic materials 0.000 claims description 15
- 239000001301 oxygen Substances 0.000 claims description 15
- 238000009826 distribution Methods 0.000 claims description 12
- 239000000446 fuel Substances 0.000 claims description 11
- 239000002918 waste heat Substances 0.000 claims description 9
- 239000000654 additive Substances 0.000 claims description 8
- 238000012544 monitoring process Methods 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 7
- 230000000996 additive effect Effects 0.000 claims description 6
- 238000013461 design Methods 0.000 claims description 4
- 230000001590 oxidative effect Effects 0.000 claims description 4
- 239000007800 oxidant agent Substances 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 2
- 238000011155 quantitative monitoring Methods 0.000 claims 1
- 229910018072 Al 2 O 3 Inorganic materials 0.000 abstract description 12
- 239000000843 powder Substances 0.000 abstract description 8
- 238000000605 extraction Methods 0.000 abstract description 6
- 230000009286 beneficial effect Effects 0.000 abstract description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 14
- 239000000377 silicon dioxide Substances 0.000 description 6
- 238000002360 preparation method Methods 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 3
- 230000007774 longterm Effects 0.000 description 3
- 239000002910 solid waste Substances 0.000 description 3
- 239000006004 Quartz sand Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 239000003250 coal slurry Substances 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012717 electrostatic precipitator Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/001—Dry processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B21/00—Obtaining aluminium
- C22B21/0007—Preliminary treatment of ores or scrap or any other metal source
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B21/00—Obtaining aluminium
- C22B21/0038—Obtaining aluminium by other processes
- C22B21/0069—Obtaining aluminium by other processes from scrap, skimmings or any secondary source aluminium, e.g. recovery of alloy constituents
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/10—Arrangements for using waste heat
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
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Abstract
本发明公开了一种用高铝煤制备铝硅粉的方法，包括利用制备铝硅粉的反应系统来制备铝硅粉；所述反应系统包括水煤浆供给系统、脱碳反应系统和铝硅粉回收系统；所述水煤浆供给系统用于向所述脱碳反应系统供给水煤浆；所述脱碳反应系统包括脱碳反应器、点火燃烧器、点火风道、旋风分离器和返料器；所述铝硅粉回收系统通过烟气道连接至所述旋风分离器的顶部烟气出口，用于进一步分离出来自旋风分离器的烟气中的粉尘以得到铝硅粉产品；本发明制出的铝硅粉含碳量低，铝硅粉中γ‑Al2O3高，有利于后续氧化铝的提取，实现了高铝煤中铝硅粉的资源化利用。
The invention discloses a method for preparing aluminum-silicon powder from high-alumina coal, which comprises using a reaction system for preparing aluminum-silicon powder to prepare aluminum-silicon powder; the reaction system includes a coal-water slurry supply system, a decarbonization reaction system and an aluminum-silicon powder powder recovery system; the coal water slurry supply system is used to supply coal water slurry to the decarbonization reaction system; the decarbonization reaction system includes a decarbonization reactor, an ignition burner, an ignition air duct, a cyclone separator and a return feeder; the alumina-silicon powder recovery system is connected to the top flue gas outlet of the cyclone separator through a flue gas channel, and is used to further separate the dust in the flue gas from the cyclone separator to obtain alumina-silicon powder products; The aluminum-silicon powder produced by the invention has low carbon content and high γ-Al 2 O 3 in the aluminum-silicon powder, which is beneficial to the subsequent extraction of alumina and realizes the resource utilization of the aluminum-silicon powder in high-alumina coal.
Description
技术领域technical field
本发明涉及煤炭资源化利用领域，尤其涉及一种用高铝煤制备铝硅粉的方法。The invention relates to the field of coal resource utilization, in particular to a method for preparing aluminum-silicon powder from high-alumina coal.
背景技术Background technique
我国内蒙地区有大量的高铝煤，该煤种灰分中Al2O3含量高达55％，目前该煤种主要应用于传统火电厂动力燃料燃烧，然而由于在火电厂燃烧温度过高、燃烧温度变化范围大等因素，导致燃烧后灰分(主要为铝硅粉)中氧化铝晶体结构均一性较差，并且大部分的氧化铝为α-Al2O3，而α-Al2O3在后续固废利用时很难从灰渣中提取，同时灰分中含碳量也偏高，对灰渣综合利用造成很大的影响。There is a large amount of high-aluminum coal in Inner Mongolia, and the content of Al 2 O 3 in the ash of this coal is as high as 55%. At present, this coal is mainly used in the combustion of power fuel in traditional thermal power plants. However, due to the high combustion temperature and Factors such as large variation range lead to poor uniformity of alumina crystal structure in post-combustion ash (mainly alumina-silicon powder), and most of alumina is α-Al 2 O 3 , and α-Al 2 O 3 in the subsequent It is difficult to extract solid waste from ash and slag, and the carbon content in ash is also high, which has a great impact on the comprehensive utilization of ash and slag.
因此，有必要开发一种合理的高铝煤处理方式，一方面使其脱碳反应温度控制在一定的范围(820℃-870℃)，另一方面控制产生的灰分中的含碳量小于5％，则非常有利于后续进一步提取氧化铝。Therefore, it is necessary to develop a reasonable high-alumina coal treatment method, on the one hand, to control the decarburization reaction temperature within a certain range (820°C-870°C), and on the other hand, to control the carbon content in the generated ash to less than 5 %, it is very beneficial to the subsequent further extraction of alumina.
发明内容Contents of the invention
为弥补现有技术中存在的不足，本发明提供一种用高铝煤制备铝硅粉的方法。In order to make up for the deficiencies in the prior art, the invention provides a method for preparing alumina-silicon powder from high-alumina coal.
为了实现上述发明目的，本发明采用了如下的技术方案：In order to realize the foregoing invention object, the present invention adopts following technical scheme:
一种用高铝煤制备铝硅粉的方法，包括利用制备铝硅粉的反应系统来制备铝硅粉；所述反应系统包括水煤浆供给系统、脱碳反应系统和铝硅粉回收系统；其中：A method for preparing aluminum-silicon powder from high-alumina coal, comprising preparing aluminum-silicon powder using a reaction system for preparing aluminum-silicon powder; the reaction system includes a coal-water slurry supply system, a decarbonization reaction system, and an aluminum-silicon powder recovery system; in:
所述水煤浆供给系统用于向所述脱碳反应系统供给水煤浆；The coal-water slurry supply system is used to supply coal-water slurry to the decarbonization reaction system;
所述脱碳反应系统包括脱碳反应器、点火燃烧器、点火风道、旋风分离器和返料器；其中：The decarburization reaction system includes a decarburization reactor, an ignition burner, an ignition air duct, a cyclone separator and a feeder; wherein:
所述点火风道的一端设置有点火燃烧器，另一端连接至所述脱碳反应器的下端，并且所述点火风道与脱碳反应器的连接处还设置有布风板，用于使所述点火风道供应的风均匀送入脱碳反应器；One end of the ignition air duct is provided with an ignition burner, and the other end is connected to the lower end of the decarburization reactor, and the junction of the ignition air duct and the decarburization reactor is also provided with an air distribution plate for making the The wind supplied by the ignition air duct is evenly sent into the decarburization reactor;
所述脱碳反应器呈立式长筒型，用于对来自所述水煤浆供给系统的水煤浆进行氧化燃烧以脱除其中的碳，所述脱碳反应器下部位于布风板的上方设有水煤浆进料口和返料器返料口、顶部设有烟气出口；The decarbonization reactor is a vertical long tube type, and is used to oxidize and burn the coal water slurry from the coal water slurry supply system to remove the carbon therein. The lower part of the decarbonization reactor is located at the There is a coal water slurry inlet and a feeder return inlet on the top, and a flue gas outlet on the top;
所述旋风分离器连接至脱碳反应器的顶部，用于部分脱除来自所述脱碳反应器的烟气中夹带的灰粒；The cyclone separator is connected to the top of the decarbonization reactor for partially removing ash particles entrained in the flue gas from the decarbonization reactor;
所述返料器设置在所述旋风分离器的下方，用于将接受的经所述旋风分离器分离出的灰粒经所述返料器返料口送回所述脱碳反应器；The feeder is arranged below the cyclone separator, and is used to send the ash particles separated by the cyclone separator back to the decarbonization reactor through the return port of the feeder;
所述铝硅粉回收系统通过烟气道连接至所述旋风分离器的顶部烟气出口，用于进一步分离出来自旋风分离器的烟气中的粉尘以得到铝硅粉产品。The alumina silica powder recovery system is connected to the top flue gas outlet of the cyclone separator through a flue gas channel, and is used to further separate the dust in the flue gas from the cyclone separator to obtain alumina silica powder products.
根据本发明的方法的一种实施方式，所述反应系统在启动时，首先在所述布风板上添加启动床料，比如循环灰或石英砂等，开启点火燃烧器；当脱碳反应器内部温度达到450℃以上时，比如500℃或550℃，向脱碳反应器内给入水煤浆，水煤浆给入量不超过满负荷设计工况的30％，比如20％或25％，并监测烟气道中含氧量的变化情况；当含氧量下降超过20％时，比如30％、40％或50％时，逐步加大水煤浆给浆量以升高脱碳反应器温度；According to one embodiment of the method of the present invention, when the reaction system is started, first add a start-up bed material on the air distribution plate, such as circulating ash or quartz sand, etc., and start the ignition burner; when the decarbonization reactor When the internal temperature reaches above 450°C, such as 500°C or 550°C, feed the coal-water slurry into the decarburization reactor, and the amount of coal-water slurry fed should not exceed 30% of the full-load design condition, such as 20% or 25%, And monitor the change of oxygen content in the flue gas channel; when the oxygen content drops by more than 20%, such as 30%, 40% or 50%, gradually increase the amount of coal water slurry to increase the temperature of the decarburization reactor ;
当脱碳反应器内部温度达到700℃-780℃时，比如720℃、750℃或760℃，逐步减少点火燃烧器的燃料供应，当脱碳反应器内部温度达到800℃-870℃之间时，比如820℃、840℃或860℃，则完全切除燃料供应。When the internal temperature of the decarbonization reactor reaches 700°C-780°C, such as 720°C, 750°C or 760°C, gradually reduce the fuel supply of the ignition burner, when the internal temperature of the decarbonization reactor reaches between 800°C-870°C , such as 820°C, 840°C or 860°C, the fuel supply is completely cut off.
根据本发明的方法的一种实施方式，所述烟气道上沿气流方向还依次设有余热回收装置和空气预热装置，所述余热回收装置用于利用烟气热量加热循环水，所述空气预热装置用于利用烟气热量对待送入所述脱碳反应器作为氧化剂的空气进行预热；所述空气预热装置包括依次设置的一次风预热装置和二次风预热装置，所述一次风预热装置与所述点火燃烧器和点火风道连接，用于预热空气并作为一次风送入所述点火燃烧器和点火风道；所述二次预热装置连接至所述脱碳反应器下部位于布风板上方且低于水煤浆进料口和返料器返料口的位置，用于预热空气并作为二次风送入所述脱碳反应器。According to one embodiment of the method of the present invention, a waste heat recovery device and an air preheating device are sequentially arranged on the flue gas channel along the airflow direction, the waste heat recovery device is used to heat the circulating water with the heat of the flue gas, and the air The preheating device is used to preheat the air to be sent into the decarbonization reactor as an oxidant by using the heat of the flue gas; the air preheating device includes a primary air preheating device and a secondary air preheating device arranged in sequence, so The primary air preheating device is connected with the ignition burner and the ignition air duct, and is used to preheat the air and send it into the ignition burner and the ignition air duct as primary air; the secondary preheating device is connected to the The lower part of the decarbonization reactor is located above the air distribution plate and lower than the coal-water slurry inlet and the return inlet of the feeder, and is used for preheating air and sending it into the decarbonization reactor as secondary air.
根据本发明的方法的一种实施方式，所述反应系统稳定时，所述脱碳反应器底部一次风占总风量比例控制在35％-45％、二次风占总风量比例相应的控制在55％-65％；所述烟气道中烟气含氧量控制在2.0％-3.0％，反应器内温度控制在820℃-870℃。According to one embodiment of the method of the present invention, when the reaction system is stable, the proportion of primary air at the bottom of the decarburization reactor to the total air volume is controlled at 35%-45%, and the proportion of secondary air to the total air volume is correspondingly controlled at 55%-65%; the oxygen content of the flue gas in the flue gas channel is controlled at 2.0%-3.0%, and the temperature in the reactor is controlled at 820°C-870°C.
根据本发明的方法的一种实施方式，将所述脱碳反应器从顶部至下部之间占所述脱碳反应器高度70％的区域的压差维持0.5-1.0kPa的范围，比如0.6或0.8kPa；当所述压差低于所述范围的下限时，向所述脱碳反应器内添加煤矸石经破碎后的细粒以使所述压差升高；当所述压差高于所述范围的上限时，减少所述返料器的返料量。According to one embodiment of the method of the present invention, the pressure difference in the area accounting for 70% of the height of the decarburization reactor between the top and the bottom of the decarburization reactor is maintained in the range of 0.5-1.0kPa, such as 0.6 or 0.8kPa; when the pressure difference is lower than the lower limit of the range, add the crushed fine particles of coal gangue to the decarburization reactor to increase the pressure difference; when the pressure difference is higher than When the upper limit of the range, reduce the return amount of the feeder.
在一种实施方式中，所述脱碳反应器的下部还设有煤矸石添加口，用于向所述脱碳反应器内添加煤矸石经破碎后的细粒；优选地，所述煤矸石添加口设置在与所述返料器返料口平齐的位置。由于水煤浆粒度较细，长时间运行后颗粒逐步磨损变细均由旋风分离器出口由烟气带出脱碳反应系统，因此运行过程中设计补充一定的添加物料维持脱碳反应器、旋风分离器、返料器组成的主循环回路的灰粒循环，在高铝煤生产中所得的煤矸石是很好的添加物料选择，将煤矸石破碎成3mm以下的细颗粒，比如0.1mm-3mm，当反应器上下部之间压差较小时，可加入一定量的煤矸石以保证主循环回路的灰粒浓度，同时煤矸石中由于同样铝灰分较高，因此矸石的添加在消纳处置矸石固废的同时也增加了铝硅粉的产量，研究表明由煤矸石脱碳反应后产生的铝硅粉品质与高铝煤产生的铝硅粉品质相当。在一种实施方式中，所述返料器上还设有煤矸石添加口，用于向所述脱碳反应器内添加煤矸石经破碎后的细粒。In one embodiment, the lower part of the decarbonization reactor is also provided with a coal gangue addition port for adding crushed coal gangue fine particles into the decarbonization reactor; preferably, the coal gangue The addition port is set at a position flush with the return port of the feeder. Due to the fine particle size of the coal water slurry, after long-term operation, the particles gradually wear and become thinner, and are taken out of the decarbonization reaction system by the flue gas at the outlet of the cyclone separator. The ash particle circulation of the main circulation loop composed of the separator and the feeder, the coal gangue obtained in the production of high-alumina coal is a good choice of additive materials, and the coal gangue is broken into fine particles below 3mm, such as 0.1mm-3mm , when the pressure difference between the upper and lower parts of the reactor is small, a certain amount of gangue can be added to ensure the concentration of ash particles in the main circulation loop. The solid waste also increases the output of alumina-silicon powder. Studies have shown that the quality of alumina-silicon powder produced by the decarburization reaction of coal gangue is equivalent to the quality of alumina-silicon powder produced by high-alumina coal. In one embodiment, the feeder is also provided with a coal gangue adding port for adding crushed coal gangue fine particles into the decarbonization reactor.
根据本发明的方法的一种实施方式，所述水煤浆中，原煤粒度＜180μm，原煤含量65-70％，水分含量29-34％，添加剂含量0.5-1.5％，热值控制在2800-3400kCal/kg，以便更好的在脱碳反应器中反应脱碳并控制反应器温度获得更多γ-Al2O3。According to one embodiment of the method of the present invention, in the coal water slurry, the raw coal particle size is <180 μm, the raw coal content is 65-70%, the moisture content is 29-34%, the additive content is 0.5-1.5%, and the calorific value is controlled at 2800- 3400kCal/kg, in order to better react decarburization in the decarburization reactor and control the temperature of the reactor to obtain more γ-Al 2 O 3 .
在一种实施方式中，所述水煤浆供给系统包括水煤浆储罐和水煤浆泵，所述水煤浆泵用于将来自水煤浆储罐中的水煤浆送入所述脱碳反应器。In one embodiment, the coal-water slurry supply system includes a coal-water slurry storage tank and a coal-water slurry pump, and the coal-water slurry pump is used to send the coal-water slurry from the coal-water slurry storage tank into the decarbonization reactor.
在一种实施方式中，所述铝硅粉回收系统包括除尘器和铝硅粉储仓，所述除尘器与所述烟气道连接，用于分离来自所述烟气道的烟气中的粉尘，所述铝硅粉储仓用于接收经所述除尘器分离得到的粉尘作为铝硅粉产品。In one embodiment, the alumina-silicon powder recovery system includes a dust collector and an alumina-silicon powder storage bin, and the dust collector is connected to the flue gas channel for separating Dust, the alumina-silicon powder storage bin is used to receive the dust separated by the dust collector as alumina-silicon powder product.
采用上述的技术方案，具有如下的技术效果：Adopt above-mentioned technical scheme, have following technical effect:
1、本发明采用水煤浆为原料，经该反应系统制备的铝硅粉粒度小于50μm，更利于后续工艺提铝；1. The present invention uses coal-water slurry as a raw material, and the particle size of the aluminum-silicon powder prepared by the reaction system is less than 50 μm, which is more conducive to the extraction of aluminum in the subsequent process;
2、本发明反应系统可使水煤浆在主反应器内足够的停留时间，脱碳反应完全，使铝硅粉中含碳量较低；同时采用水煤浆原料，该反应系统可使主反应器内温度维持820℃-870℃之间，使高铝煤脱碳反应后铝硅粉中Al2O3更多的转化为γ-Al2O3，有利于后续工艺铝硅粉提取铝；2. The reaction system of the present invention can make the coal-water slurry stay in the main reactor for a sufficient time, and the decarburization reaction is complete, so that the carbon content in the aluminum-silicon powder is low; The temperature in the reactor is maintained between 820°C and 870°C, so that more Al 2 O 3 in the aluminum silicon powder can be converted into γ-Al 2 O 3 after the decarburization reaction of high-alumina coal, which is beneficial to the subsequent process of aluminum silicon powder extraction of aluminum ;
3、本发明的反应系统还设计有回收烟气余热的装置，系统热效率高；将高铝煤制备成热值稳定的水煤浆，保证进入脱碳反应器的水煤浆连续稳定；3. The reaction system of the present invention is also designed with a device for recovering waste heat of flue gas, and the thermal efficiency of the system is high; high-aluminum coal is prepared into coal-water slurry with stable calorific value, ensuring continuous and stable coal-water slurry entering the decarbonization reactor;
4、采用高效的旋风分离器进行分离时，可有效分离烟气中较大或较重颗粒，而为未脱碳完全的颗粒由于未经充分高温反应而不易细化，因此可对未脱碳完全的颗粒进行有效分离；采用脱碳反应器、旋风分离器及返料器组成的循环回路燃烧方式，增加碳在反应器内停留时间，降低铝硅粉中含碳量。制出的铝硅粉含碳量可控制在2％—4％之间，铝硅粉中γ-Al2O3占总Al2O3比例大于80％。4. When the high-efficiency cyclone separator is used for separation, the larger or heavier particles in the flue gas can be effectively separated, and the particles that are not completely decarburized are not easy to be refined due to insufficient high-temperature reaction, so the non-decarbonized particles can be separated The complete particles are effectively separated; the circulation loop combustion method composed of decarbonization reactor, cyclone separator and feeder is adopted to increase the residence time of carbon in the reactor and reduce the carbon content in aluminum silicon powder. The carbon content of the prepared aluminum-silicon powder can be controlled between 2% and 4%, and the proportion of γ-Al 2 O 3 to the total Al 2 O 3 in the aluminum-silicon powder is greater than 80%.
附图说明Description of drawings
图1为本发明所采用的反应系统的一种实施方式的示意图。Fig. 1 is a schematic diagram of an embodiment of the reaction system used in the present invention.
图中部分标号说明如下：标号1：水煤浆制备系统、标号2：水煤浆储罐、标号3：水煤浆泵、标号4：流量计、标号5：点火燃烧器、标号6：点火风道、标号7：脱碳反应器、标号8：旋风分离器、标号10：返料器、标号11：布风板、标号12：烟气道、标号13：余热回收装置、标号14：一次风预热装置、标号15：一次风机、标号16：除尘器、标号17：铝硅粉储仓、标号18：二次风机、标号19：二次风预热装置、标号21：压差监测点、标号22、温度监测点、标号23：氧量监测点。Some labels in the figure are explained as follows: label 1: coal water slurry preparation system, label 2: coal water slurry storage tank, label 3: coal water slurry pump, label 4: flow meter, label 5: ignition burner, label 6: ignition Air channel, label 7: decarbonization reactor, label 8: cyclone separator, label 10: feeder, label 11: air distribution plate, label 12: flue gas channel, label 13: waste heat recovery device, label 14: primary Air preheating device, label 15: primary fan, label 16: dust collector, label 17: aluminum silicon powder storage bin, label 18: secondary fan, label 19: secondary air preheating device, label 21: differential pressure monitoring point , label 22, temperature monitoring point, label 23: oxygen monitoring point.
具体实施方式Detailed ways
为了更好的理解本发明的技术方案，下面结合实施例进一步阐述本发明的内容，但本发明的内容并不仅仅局限于以下实施例。在本发明中，如未特别说明，文中的百分数或百分含量均为质量百分数或质量百分含量。In order to better understand the technical solution of the present invention, the content of the present invention will be further described below in conjunction with the examples, but the content of the present invention is not limited only to the following examples. In the present invention, unless otherwise specified, the percentages or percentages herein are all mass percentages or mass percentages.
如图1所示，本发明用高铝煤制备铝硅粉的方法，包括利用制备铝硅粉的反应系统来制备铝硅粉，所述反应系统用于将高铝煤进行脱碳反应后制铝硅粉，包括水煤浆供给系统、脱碳反应系统和铝硅粉回收系统。As shown in Figure 1, the method for preparing aluminum-silicon powder from high-alumina coal in the present invention includes using a reaction system for preparing aluminum-silicon powder to prepare aluminum-silicon powder, and the reaction system is used to prepare high-alumina coal after decarbonization Aluminum silicon powder, including coal water slurry supply system, decarbonization reaction system and aluminum silicon powder recovery system.
其中，所述水煤浆供给系统用于向所述脱碳反应系统供给水煤浆，包括水煤浆储罐和水煤浆泵，所述水煤浆泵用于将来自水煤浆储罐中的水煤浆送入所述脱碳反应器。来自水煤浆制备系统1的水煤浆经管道与水煤浆储罐2进口相连，水煤浆储罐2出口经管道与水煤浆泵3进口相连，水煤浆泵3出口经管道与脱碳反应器7相连，在水煤浆泵3出口与脱碳反应器7连接管道上设置有流量计4。水煤浆制备由水煤浆制备系统1完成，将比如来自内蒙地区的高铝煤磨成200μm以下的煤粉，然后以一定的比例和水混合后加入添加剂制成水煤浆，合格的水煤浆储存在水煤浆储罐2中，铝硅粉制备过程中水煤浆由水煤浆泵3增压送入脱碳反应器7，流量计4可以对水煤浆量进行精准计量。Wherein, the coal-water slurry supply system is used to supply coal-water slurry to the decarbonization reaction system, including a coal-water slurry storage tank and a coal-water slurry pump, and the coal-water slurry pump is used to supply the coal-water slurry from the coal-water slurry storage tank The coal water slurry in is sent to the decarbonization reactor. The coal water slurry from the coal water slurry preparation system 1 is connected to the inlet of the coal water slurry storage tank 2 through the pipeline, the outlet of the coal water slurry storage tank 2 is connected to the inlet of the coal water slurry pump 3 through the pipeline, and the outlet of the coal water slurry pump 3 is connected to the inlet of the coal water slurry pump 3 through the pipeline. The decarbonization reactor 7 is connected, and a flow meter 4 is arranged on the connecting pipe between the outlet of the coal-water slurry pump 3 and the decarbonization reactor 7 . The preparation of coal-water slurry is completed by the coal-water slurry preparation system 1. For example, high-alumina coal from Inner Mongolia is ground into coal powder below 200 μm, and then mixed with water in a certain proportion and then added with additives to make coal-water slurry. Qualified water The coal slurry is stored in the coal water slurry storage tank 2. During the preparation of aluminum silicon powder, the coal water slurry is pressurized by the coal water slurry pump 3 and sent to the decarbonization reactor 7. The flow meter 4 can accurately measure the amount of the coal water slurry.
所述水煤浆中，原煤粒度＜180μm，比如200μm或250μm，原煤含量65-70％，比如68％，水分含量29-34％比如31％，添加剂含量0.5-1.5％比如1％，热值控制在2800-3400kCal/kg比如3100kCal/kg，以便更好的在脱碳反应器中反应脱碳并控制反应器温度获得更多γ-Al2O3。In the coal water slurry, the raw coal particle size is <180 μm, such as 200 μm or 250 μm, the raw coal content is 65-70%, such as 68%, the moisture content is 29-34%, such as 31%, the additive content is 0.5-1.5%, such as 1%, and the calorific value Control it at 2800-3400kCal/kg, such as 3100kCal/kg, so as to better react decarburization in the decarburization reactor and control the temperature of the reactor to obtain more γ-Al 2 O 3 .
所述脱碳反应系统包括脱碳反应器7、点火燃烧器5、点火风道6、旋风分离器8和返料器10；其中：所述点火风道6的一端设置有点火燃烧器5，另一端连接至所述脱碳反应器7的下端，并且所述点火风道6与脱碳反应器7的连接处还设置有布风板11，用于使所述点火风道供应的风均匀送入脱碳反应器；所述脱碳反应器7呈立式长筒型，用于对来自所述水煤浆供给系统的水煤浆进行氧化燃烧以脱除其中的碳，所述脱碳反应器7下部位于布风板11的上方设有水煤浆进料口和返料器返料口、顶部设有烟气出口；所述旋风分离器8连接至脱碳反应器7的顶部，用于部分脱除来自所述脱碳反应器的烟气中夹带的灰粒；所述返料器10设置在所述旋风分离器的下方，用于将接受的经所述旋风分离器分离出的灰粒经所述返料器返料口送回所述脱碳反应器。The decarburization reaction system includes a decarburization reactor 7, an ignition burner 5, an ignition air duct 6, a cyclone separator 8 and a feeder 10; wherein: one end of the ignition air duct 6 is provided with an ignition burner 5, The other end is connected to the lower end of the decarburization reactor 7, and the junction of the ignition air duct 6 and the decarburization reactor 7 is also provided with an air distribution plate 11, which is used to make the wind supplied by the ignition air duct uniform Send into the decarbonization reactor; the decarbonization reactor 7 is a vertical long tube type, and is used to oxidize and burn the coal water slurry from the described coal water slurry supply system to remove the carbon therein, and the decarburization The lower part of the reactor 7 is located above the air distribution plate 11 and is provided with a coal-water slurry inlet and a feeder return inlet, and the top is provided with a flue gas outlet; the cyclone separator 8 is connected to the top of the decarbonization reactor 7, It is used to partially remove the ash particles entrained in the flue gas from the decarbonization reactor; the return feeder 10 is arranged below the cyclone separator, and is used to separate the received gas from the cyclone separator The ash particles are sent back to the decarbonization reactor through the return port of the feeder.
点火燃烧器5为启动阶段设备预热所用，可采用天然气或油作为燃料，将脱碳反应器7内温度加热至水煤浆着火温度以上，保证给入脱碳反应器7的水煤浆稳定着火；在运行阶段，也可根据需要点火，或不点火。点火风道6使点火时点火燃烧器5产生的热烟气及空气混合均匀，脱碳反应器7为水煤浆进行氧化脱碳反应，旋风分离器8将反应器出口携带的未脱碳颗粒的烟气进行气固分离，被分离的未脱碳颗粒经返料器10重新返回脱碳反应器7进行循环燃烧脱碳，未分离的细颗粒及烟气由旋风分离器8顶部烟气出口进入烟气道12。The ignition burner 5 is used for equipment preheating in the start-up phase. Natural gas or oil can be used as fuel to heat the temperature inside the decarbonization reactor 7 to above the ignition temperature of the coal-water slurry to ensure the stability of the coal-water slurry fed into the decarbonization reactor 7. Ignition; during the operation phase, it can also be ignited or not ignited according to needs. The ignition duct 6 makes the hot flue gas and air generated by the ignition burner 5 mix evenly during ignition, the decarburization reactor 7 is the coal-water slurry for oxidative decarburization reaction, and the cyclone separator 8 removes the non-decarbonized particles carried by the reactor outlet The flue gas is subjected to gas-solid separation, and the separated non-decarburized particles are returned to the decarbonization reactor 7 through the feeder 10 for circular combustion decarbonization, and the unseparated fine particles and flue gas are discharged from the flue gas outlet at the top of the cyclone separator 8 Enter the flue gas channel 12.
所述反应系统在启动时，首先在所述布风板上添加启动床料，比如循环灰或石英砂等，开启点火燃烧器；当脱碳反应器内部温度达到450℃以上时，比如500℃或550℃，向脱碳反应器内给入水煤浆，水煤浆给入量不超过满负荷设计工况的30％，比如20％或25％，并监测烟气道中含氧量的变化情况；当含氧量下降超过20％时，比如30％、40％或50％时，逐步加大水煤浆给浆量以升高脱碳反应器温度；When the reaction system is started, firstly, start-up bed material, such as circulating ash or quartz sand, etc. is added to the air distribution plate, and the ignition burner is turned on; when the internal temperature of the decarburization reactor reaches above 450°C, such as 500°C or 550°C, feed coal water slurry into the decarburization reactor, the amount of coal water slurry fed does not exceed 30% of the full load design condition, such as 20% or 25%, and monitor the change of oxygen content in the flue gas channel ;When the oxygen content drops by more than 20%, such as 30%, 40% or 50%, gradually increase the amount of coal water slurry to increase the temperature of the decarburization reactor;
当脱碳反应器内部温度达到700℃-780℃时，比如720℃、750℃或760℃，逐步减少点火燃烧器的燃料供应，当脱碳反应器内部温度达到800℃-870℃之间时，比如820℃、840℃或860℃，则完全切除燃料供应。When the internal temperature of the decarbonization reactor reaches 700°C-780°C, such as 720°C, 750°C or 760°C, gradually reduce the fuel supply of the ignition burner, when the internal temperature of the decarbonization reactor reaches between 800°C-870°C , such as 820°C, 840°C or 860°C, the fuel supply is completely cut off.
所述铝硅粉回收系统通过烟气道连接至所述旋风分离器的顶部烟气出口，用于进一步分离出来自旋风分离器的烟气中的粉尘以得到铝硅粉产品。所述烟气道上沿气流方向还依次设有余热回收装置13和空气预热装置，所述余热回收装置用于利用烟气热量加热循环水，所述空气预热装置用于利用烟气热量对待送入所述脱碳反应器作为氧化剂的空气进行预热。所述空气预热装置包括依次设置的一次风预热装置14和二次风预热装置19，所述一次风预热装置14接收来自一次分机15供给的空气，并与所述点火燃烧器5和点火风道连接6，用于预热空气作为一次风并送入所述点火燃烧器5和点火风道6，本领域技术人员理解，当反应系统运行稳定点火燃烧器5关闭时，来自一次风预热装置14的预热空气可全部送入点火风道6；所述二次预热装置19接收来自二次分机18供给的空气，并连接至所述脱碳反应器7下部位于布风板11上方且低于水煤浆进料口和返料器返料口的位置，用于预热空气并作为二次风送入所述脱碳反应器。The alumina silica powder recovery system is connected to the top flue gas outlet of the cyclone separator through a flue gas channel, and is used to further separate the dust in the flue gas from the cyclone separator to obtain alumina silica powder products. Along the airflow direction, the flue gas channel is also provided with a waste heat recovery device 13 and an air preheating device in sequence. The air fed to the decarburization reactor as oxidant is preheated. The air preheating device includes a primary air preheating device 14 and a secondary air preheating device 19 arranged in sequence. The primary air preheating device 14 receives the air supplied from the primary extension 15 and is connected with the ignition burner 5 It is connected with the ignition air duct 6, and is used for preheating air as the primary air and is sent into the ignition burner 5 and the ignition air duct 6. Those skilled in the art understand that when the reaction system runs stably and the ignition burner 5 is closed, from the primary air The preheated air of the air preheating device 14 can all be sent into the ignition air duct 6; the secondary preheating device 19 receives the air supplied from the secondary extension 18, and is connected to the lower part of the decarbonization reactor 7 and is located in the air distribution The position above the plate 11 and below the coal water slurry inlet and the feeder return inlet is used for preheating air and sending it into the decarbonization reactor as secondary air.
所述铝硅粉回收系统包括除尘器16和铝硅粉储仓17，所述除尘器16与所述烟气道12连接，用于分离来自所述烟气道12的烟气中的粉尘，比如可以是旋风除尘器、静电除尘器或布袋除尘器。所述铝硅粉储仓17用于接收经所述除尘器16分离得到的粉尘作为铝硅粉产品。除尘器16底部与铝硅粉储仓17相连，除尘器16出口为排烟管，烟气经余热回收装置和空气预热装置冷却后进入除尘器16，铝硅粉被除尘器16分离后储存在铝硅粉储仓17为后续提取铝所用，洁净的烟气由除尘器16出口经排烟管排出。The aluminum silicon powder recovery system includes a dust collector 16 and an aluminum silicon powder storage bin 17, and the dust collector 16 is connected to the flue gas channel 12 for separating the dust from the flue gas of the flue gas channel 12, Examples may be cyclones, electrostatic precipitators or baghouses. The alumina silica powder storage bin 17 is used to receive the dust separated by the dust collector 16 as alumina silica powder product. The bottom of the dust collector 16 is connected with the aluminum silicon powder storage bin 17. The outlet of the dust collector 16 is a smoke exhaust pipe. The flue gas enters the dust collector 16 after being cooled by the waste heat recovery device and the air preheating device. The aluminum silicon powder is separated by the dust collector 16 and then stored. The aluminum-silicon powder storage bin 17 is used for the subsequent extraction of aluminum, and the clean flue gas is discharged from the outlet of the dust collector 16 through the exhaust pipe.
所述脱碳反应器由上之下设有多个压力监测点和多个温度监测点22，以便监测反应器内温度和压差。所述烟气道上还设有氧量监测点23，以便监测烟气中的含氧量。The decarburization reactor is provided with a plurality of pressure monitoring points and a plurality of temperature monitoring points 22 from top to bottom, so as to monitor the temperature and pressure difference in the reactor. An oxygen monitoring point 23 is also provided on the flue gas channel to monitor the oxygen content in the flue gas.
所述反应系统稳定时，所述脱碳反应器底部一次风占总风量比例控制在35％-45％比如40％、二次风占总风量比例相应的控制在55％-65％比如60％；所述烟气道中烟气含氧量控制在2.0％-3.0％，反应器内温度控制在820℃-870℃。When the reaction system is stable, the proportion of primary air at the bottom of the decarburization reactor to the total air volume is controlled at 35%-45%, such as 40%, and the proportion of secondary air to the total air volume is controlled at 55%-65%, such as 60%. ; The oxygen content of the flue gas in the flue gas channel is controlled at 2.0%-3.0%, and the temperature in the reactor is controlled at 820°C-870°C.
在一种实施方式中，所述脱碳反应器的下部还设有煤矸石添加口，用于向所述脱碳反应器内添加煤矸石经破碎后的细粒；优选地，所述煤矸石添加口设置在与所述返料器返料口平齐的位置。由于水煤浆粒度较细，长时间运行后颗粒逐步磨损变细均由旋风分离器出口由烟气带出脱碳反应系统，因此运行过程中设计补充一定的添加物料维持脱碳反应器、旋风分离器、返料器组成的主循环回路的灰粒循环，在高铝煤生产中所得的煤矸石是很好的添加物料选择，将煤矸石破碎成3mm以下的细颗粒，比如0.1mm-3mm，当反应器上下部之间压差较小时，可加入一定量的煤矸石以保证主循环回路的灰粒浓度，同时煤矸石中由于同样铝灰分较高，因此矸石的添加在消纳处置矸石固废的同时也增加了铝硅粉的产量，研究表明由煤矸石脱碳反应后产生的铝硅粉品质与高铝煤产生的铝硅粉品质相当。在一个实施例中，所述返料器上还设有煤矸石添加口，用于向所述脱碳反应器内添加煤矸石经破碎后的细粒。In one embodiment, the lower part of the decarbonization reactor is also provided with a coal gangue addition port for adding crushed coal gangue fine particles into the decarbonization reactor; preferably, the coal gangue The addition port is set at a position flush with the return port of the feeder. Due to the fine particle size of the coal water slurry, after long-term operation, the particles gradually wear and become thinner, and are taken out of the decarbonization reaction system by the flue gas at the outlet of the cyclone separator. The ash particle circulation of the main circulation loop composed of the separator and the feeder, the coal gangue obtained in the production of high-alumina coal is a good choice of additive materials, and the coal gangue is broken into fine particles below 3mm, such as 0.1mm-3mm , when the pressure difference between the upper and lower parts of the reactor is small, a certain amount of gangue can be added to ensure the concentration of ash particles in the main circulation loop. The solid waste also increases the output of alumina-silicon powder. Studies have shown that the quality of alumina-silicon powder produced by the decarburization reaction of coal gangue is equivalent to the quality of alumina-silicon powder produced by high-alumina coal. In one embodiment, the feeder is also provided with a coal gangue adding port for adding crushed coal gangue fine particles into the decarbonization reactor.
在本发明的方法中，可以将所述脱碳反应器从顶部至下部之间占所述脱碳反应器高度70％的区域的压差维持0.5-1.0kPa的范围，比如0.6或0.8kPa；当所述压差低于所述范围的下限时，向所述脱碳反应器内添加煤矸石经破碎后的细粒以使所述压差升高；当所述压差高于所述范围的上限时，减少所述返料器的返料量。In the method of the present invention, the pressure difference between the top and the bottom of the decarburization reactor, which accounts for 70% of the height of the decarburization reactor, can be maintained in the range of 0.5-1.0kPa, such as 0.6 or 0.8kPa; When the pressure difference is lower than the lower limit of the range, add the crushed fine particles of coal gangue to the decarburization reactor to increase the pressure difference; when the pressure difference is higher than the range When the upper limit, reduce the return amount of the feeder.
实施例Example
水煤浆参数如下：原煤粒度＜180μm，原煤含量68％，水分含量31％，添加剂含量1％，热值控制在3100kCal/kg；The coal water slurry parameters are as follows: raw coal particle size <180μm, raw coal content 68%, moisture content 31%, additive content 1%, calorific value controlled at 3100kCal/kg;
启动阶段在脱碳反应器布风板上添加厚度500mm的循环灰作为启动床料，点火辅助燃料采用天然气，当脱碳反应器内部温度达到460℃时，向反应器内给入水煤浆，总的水煤浆给入量可按满负荷设计的工况30％的量给入，氧量出现明显下降，水煤浆点火成功，后续逐步加大给浆量升高脱碳反应器温度。At the start-up stage, circulating ash with a thickness of 500 mm was added to the air distribution plate of the decarbonization reactor as the start-up bed material, and natural gas was used as the auxiliary fuel for ignition. The amount of coal-water slurry fed can be fed according to 30% of the full-load design working condition. The oxygen content drops significantly, and the coal-water slurry is successfully ignited. Then, gradually increase the amount of slurry fed to increase the temperature of the decarburization reactor.
当脱碳反应器内部整体温度水平达到720℃时，逐步减少辅助燃料量，观察过程中脱碳反应器内温度变化，脱碳反应器内部温度稳步上升，直至脱碳反应器内部整体温度水平达到780℃切除辅助燃料，达到纯烧水煤浆工况。When the overall temperature level inside the decarburization reactor reaches 720°C, gradually reduce the amount of auxiliary fuel, observe the temperature change in the decarbonization reactor during the process, and the internal temperature of the decarbonization reactor rises steadily until the overall temperature level inside the decarbonization reactor reaches The auxiliary fuel is removed at 780°C to achieve pure coal-water slurry heating conditions.
稳定运行时，脱碳反应器底部一次风比例控制在40％、二次风比例控制在60％，余热回收装置出口氧量控制在2.5％，反应器内温度维持在820℃-870℃，为了使反应器内上下温度均匀，保持较小的温度偏差，在运行过程中保持脱碳反应器上部(70％反应器净高)压差维持0.8kPa。由于水煤浆粒度较细，长时间运行后颗粒逐步磨损变细均由分离器出口由烟气带出脱碳反应系统，因此运行过程中需要补充一定的添加物料维持脱碳反应器、分离器、回料器组成的主循环回路的灰循环，该地区煤矸石是很好的添加物料选择，将煤矸石破碎成0.1-3mm的细粒。经检测，所得铝硅粉中γ-Al2O3含量占总Al2O3比例在83-85％，铝硅粉中含碳量在2-4％，该铝硅粉成分非常有利于后续氧化铝的提取，实现了高铝煤中铝硅粉的资源化利用。During stable operation, the proportion of primary air at the bottom of the decarburization reactor is controlled at 40%, the proportion of secondary air is controlled at 60%, the oxygen at the outlet of the waste heat recovery device is controlled at 2.5%, and the temperature in the reactor is maintained at 820°C-870°C. Make the upper and lower temperatures in the reactor uniform, keep a small temperature deviation, and keep the pressure difference at the upper part of the decarburization reactor (70% of the net height of the reactor) at 0.8kPa during operation. Due to the fine particle size of the coal water slurry, after long-term operation, the particles gradually wear and become finer and are taken out of the decarbonization reaction system by the flue gas at the outlet of the separator. Therefore, it is necessary to supplement certain additives during the operation to maintain the decarbonization reactor and separator. , The ash circulation of the main circulation loop composed of the feeder, the coal gangue in this area is a good choice for adding materials, and the coal gangue is broken into fine particles of 0.1-3mm. After testing, the content of γ-Al 2 O 3 in the obtained aluminum-silicon powder accounts for 83-85% of the total Al 2 O 3 , and the carbon content in the aluminum-silicon powder is 2-4%. The composition of the aluminum-silicon powder is very beneficial for subsequent The extraction of alumina has realized the resource utilization of aluminum silicon powder in high alumina coal.
本领域技术人员可以理解，在本说明书的教导之下，可对本发明做出一些修改或调整。这些修改或调整也应当在本发明权利要求所限定的范围之内。Those skilled in the art can understand that some modifications or adjustments can be made to the present invention under the teaching of this specification. These modifications or adjustments should also be within the scope defined by the claims of the present invention.
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