CN101638590B - A method for producing synthesis gas by chemical looping gasification of combustible solid waste and serial fluidized bed reactor - Google Patents
A method for producing synthesis gas by chemical looping gasification of combustible solid waste and serial fluidized bed reactor Download PDFInfo
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- 239000000126 substance Substances 0.000 title claims abstract description 15
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 92
- 239000001301 oxygen Substances 0.000 claims abstract description 92
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
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- 239000011261 inert gas Substances 0.000 description 1
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 description 1
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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
- 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
本发明提供了一种可燃固体废弃物化学链气化制合成气的方法及串行流化床反应器。该方法在一串行流化床反应器中实施，所述串行流化床反应器包括内部联通的燃料反应器和空气反应器。可燃固体废弃物在燃料反应器内与氧载体发生气化反应而生成合成气，可燃固体废弃物气化所需的氧元素来自氧载体分子中的晶格氧；失去晶格氧后的氧载体，被传输到空气反应器，在空气反应器中，氧载体被高温空气重新氧化，回复晶格氧；回复晶格氧后的氧载体被高速空气带出空气反应器，又返回燃料反应器循环使用，再次和可燃固体废弃物发生气化反应。本发明是一种突破了现有技术的高效的可燃固体废弃物气化技术，能制取高品质合成气，并能降低气化过程焦油、积碳含量。
The invention provides a method for producing synthesis gas by chemical chain gasification of combustible solid waste and a serial fluidized bed reactor. The method is implemented in a serial fluidized bed reactor, and the serial fluidized bed reactor includes a fuel reactor and an air reactor connected internally. The combustible solid waste reacts with the oxygen carrier in the fuel reactor to generate synthesis gas. The oxygen element required for the gasification of the combustible solid waste comes from the lattice oxygen in the oxygen carrier molecule; the oxygen carrier after losing the lattice oxygen , is transported to the air reactor, in the air reactor, the oxygen carrier is re-oxidized by the high-temperature air to restore lattice oxygen; the oxygen carrier after restoring lattice oxygen is taken out of the air reactor by high-speed air, and returns to the fuel reactor for circulation Use, gasification reaction with combustible solid waste again. The invention is a high-efficiency combustible solid waste gasification technology that breaks through the prior art, can produce high-quality synthesis gas, and can reduce tar and carbon deposition content in the gasification process.
Description
技术领域 technical field
本发明涉及新能源及可再生能源技术领域，尤其涉及一种可燃固体废弃物化学链气化制合成气的方法及串行流化床反应器。The invention relates to the technical field of new energy and renewable energy, in particular to a method for producing synthesis gas by chemical looping gasification of combustible solid waste and a serial fluidized bed reactor.
技术背景 technical background
由于化石燃料的日益减少以及化石能源利用过程带来的环境污染问题，研究、开发和利用清洁的可再生能源已经成为能源工作者的重要研究课题。目前，我国每年产生农作物秸秆8.4亿吨、年清运城市生活垃圾1.5亿吨，这其中有相当大的比例是可以作为能源原料的可燃固体废弃物。包括生物质资源在内的可燃固体废弃物具有资源量大、可再生、对环境污染小等优点，因此，研究开发新型、高效的可燃固体废弃物转化利用技术也成为新能源领域的研究热点之一。其中，可燃固体废弃物气化被认为是比较有前景的可燃固体废弃物转化技术。在一般的流化床气化反应器中，如果期望获得高热值或富氢合成气，则需要提供富氧气体或高温水蒸气作为气化剂，从而使工艺变得复杂，气化成本增高。另外，传统的可燃固体废弃物气化过程还会产生大量的焦油，不仅影响可燃固体废弃物总体气化效率，还会对反应器及配套设备产生堵塞、腐蚀等问题，这些问题也制约了可燃固体废弃物气化技术的大规模推广和利用。Due to the decrease of fossil fuels and the environmental pollution caused by the utilization of fossil energy, the research, development and utilization of clean and renewable energy have become an important research topic for energy workers. At present, my country produces 840 million tons of crop straw and 150 million tons of municipal solid waste annually, a considerable proportion of which is combustible solid waste that can be used as energy raw materials. Combustible solid waste, including biomass resources, has the advantages of large resources, renewable, and less environmental pollution. Therefore, the research and development of new and efficient combustible solid waste conversion and utilization technologies has become one of the research hotspots in the field of new energy. one. Among them, combustible solid waste gasification is considered to be a more promising combustible solid waste conversion technology. In a general fluidized bed gasification reactor, if it is desired to obtain high calorific value or hydrogen-rich synthesis gas, it is necessary to provide oxygen-enriched gas or high-temperature steam as a gasification agent, which complicates the process and increases the cost of gasification. In addition, the traditional combustible solid waste gasification process will also produce a large amount of tar, which not only affects the overall gasification efficiency of combustible solid waste, but also causes problems such as blockage and corrosion of the reactor and supporting equipment. These problems also restrict combustible solid waste. Large-scale promotion and utilization of solid waste gasification technology.
目前，虽然已经有了少量关于生物质在串行流化床内气化的报道，但在串行流化床内，采用金属氧化物为氧载体，通过化学链反应方式使可燃固体废弃物气化制合成气的过程还少见报道。At present, although there have been a few reports on the gasification of biomass in a serial fluidized bed, in a serial fluidized bed, metal oxides are used as oxygen carriers to make combustible solid waste gasify through a chemical chain reaction. The process of producing syngas is rarely reported.
发明内容 Contents of the invention
本发明的一个目的是提供一种可燃固体废弃物化学链气化制合成气的方法。An object of the present invention is to provide a method for producing syngas by chemical looping gasification of combustible solid waste.
本发明的另外一个目的在于提供所述可燃固体废弃物化学链气化制合成气的方法使用的串行流化床反应器。Another object of the present invention is to provide a serial fluidized bed reactor used in the method for producing synthesis gas by chemical looping gasification of combustible solid waste.
为达到上述目的，本发明采取了以下技术方案：In order to achieve the above object, the present invention has taken the following technical solutions:
本发明可燃固体废弃物化学链气化制备合成气的方法，其特征在于该方法在一串行流化床反应器中实施，所述串行流化床反应器包括内部联通的燃料反应器和空气反应器；燃料反应器为鼓泡流化床；空气反应器为一个流化床提升管，该方法包括以下步骤：The method for preparing synthesis gas by chemical looping gasification of combustible solid waste according to the present invention is characterized in that the method is implemented in a serial fluidized bed reactor, and the serial fluidized bed reactor includes an internally connected fuel reactor and Air reactor; The fuel reactor is a bubbling fluidized bed; The air reactor is a fluidized bed riser, and the method may further comprise the steps:
1)将可燃固体废弃物原料进行粉碎、干燥等预处理后备用；1) The combustible solid waste raw materials are pretreated by crushing, drying, etc. before being used;
2)可燃固体废弃物在燃料反应器内与氧载体发生气化反应而生成合成气，可燃固体废弃物气化所需的氧元素来自氧载体分子中的晶格氧；2) Combustible solid waste undergoes gasification reaction with oxygen carrier in the fuel reactor to generate synthesis gas, and the oxygen element required for the gasification of combustible solid waste comes from the lattice oxygen in the oxygen carrier molecule;
3)失去晶格氧后的氧载体，被传输到空气反应器，在空气反应器中，氧载体被高温空气重新氧化，回复晶格氧；3) The oxygen carrier after losing the lattice oxygen is transported to the air reactor, and in the air reactor, the oxygen carrier is re-oxidized by the high-temperature air to restore the lattice oxygen;
4)回复晶格氧后的氧载体被高速空气带出空气反应器，又返回燃料反应器循环使用，再次和可燃固体废弃物发生气化反应。4) The oxygen carrier after recovering the lattice oxygen is taken out of the air reactor by the high-speed air, and then returned to the fuel reactor for recycling, and gasification reaction occurs with combustible solid waste again.
本发明方法使用的串行流化床反应器的主体结构包括两个内部联通的流化床反应器，即燃料反应器和空气反应器；燃料反应器为鼓泡流化床，螺旋进料器与鼓泡流化床的高温区相连，鼓泡流化床的底部有布风板，流化气体经布风板上的小孔向上流动，使物料流化；鼓泡流化床的中部是扩展段，扩展段比反应段口径大，从而使气体流速降低，防止物料被气体带走；空气反应器为一个流化床提升管；在鼓泡流化床和流化床提升管之间有一个返料管联通，流化床提升管底部有布风管，物料在高温空气中反应，并被高速空气经流化床提升管带出流化床提升管，带出的物料经过旋风分离器分离出碎屑和残渣后返回鼓泡流化床；鼓泡流化床的上部开有一排气孔，产物气体从排气孔流出鼓泡流化床后经旋风分离器分离出固体残渣后通往气体净化装置。The main body structure of the serial fluidized bed reactor that the inventive method uses comprises the fluidized bed reactor of two internal communication, i.e. fuel reactor and air reactor; Fuel reactor is a bubbling fluidized bed, screw feeder Connected with the high temperature area of the bubbling fluidized bed, there is an air distribution plate at the bottom of the bubbling fluidized bed, and the fluidizing gas flows upward through the small holes on the air distribution plate to fluidize the material; the middle part of the bubbling fluidized bed is The expansion section, the expansion section has a larger diameter than the reaction section, so that the gas flow rate is reduced and the material is prevented from being carried away by the gas; the air reactor is a fluidized bed riser; there is a fluidized bed riser between the bubbling fluidized bed and the fluidized bed riser A return pipe is connected, and there is an air distribution pipe at the bottom of the fluidized bed riser. The material reacts in the high-temperature air, and is taken out of the fluidized bed riser by the high-speed air through the fluidized bed riser, and the brought out material passes through the cyclone separator. After separating debris and residue, return to the bubbling fluidized bed; there is a vent hole in the upper part of the bubbling fluidized bed, and the product gas flows out of the bubbling fluidized bed through the vent hole, and the solid residue is separated by a cyclone separator, and then passed through to the gas purification unit.
本发明方法的步骤进一步说明如下：The step of the inventive method is further described as follows:
(1)将可燃固体废弃物原料进行粉碎、干燥等预处理后备用；(1) Pretreatment of combustible solid waste raw materials such as pulverization and drying for later use;
所述可燃固体废弃物原料包括农作物秸秆、农林加工废弃物、城市生活垃圾可燃组分等。The combustible solid waste raw materials include crop stalks, agricultural and forestry processing waste, combustible components of urban domestic waste, and the like.
(2)氧载体由过渡金属氧化物、惰性载体和粘结剂制备而成，将制备好的氧载体颗粒预先装填在鼓泡流化床内充当床料，开启流化床外加热电源，将床料预热到指定温度，一般情况下，可将床料加热并稳定在500-900℃范围内；(2) The oxygen carrier is prepared from a transition metal oxide, an inert carrier and a binder. The prepared oxygen carrier particles are pre-packed in a bubbling fluidized bed as a bed material, and the external heating power of the fluidized bed is turned on. The bed material is preheated to the specified temperature. Generally, the bed material can be heated and stabilized within the range of 500-900°C;
所述制备氧载体的过渡金属氧化物包括但不限于NiO，CuO，Fe2O3，Mn3O4；所述制备氧载体的惰性载体包括但不限于Al2O3，SiO2，MgO，NiAl2O4，MgAl2O4，ZrO2；所述制备氧载体的粘结剂包括但不限于Al2O3，SiO2，YSZ。The transition metal oxides for preparing oxygen carriers include but are not limited to NiO, CuO, Fe 2 O 3 , Mn 3 O 4 ; the inert carriers for preparing oxygen carriers include but are not limited to Al 2 O 3 , SiO 2 , MgO, NiAl 2 O 4 , MgAl 2 O 4 , ZrO 2 ; the binder for preparing the oxygen carrier includes but not limited to Al 2 O 3 , SiO 2 , YSZ.
(3)采用水蒸气作为流化气体，从鼓泡流化床底部通入，使氧载体实现流态化，待床料的温度、流化都稳定后，可燃固体废弃物原料通过螺旋进料器加入鼓泡流化床中的床料中，可燃固体废弃物原料受热后迅速发生脱水、热解、气化等反应，气体产物、焦油和固定碳继续和氧载体发生反应，使固体废弃物进一步气化。气化产物由鼓泡流化床顶部导出，经过净化后进一步利用。气体产物组分可通过气体取样口采样进行分析，根据分析结果，可进一步调节气化温度、氧载体/可燃固体废弃物比率、水蒸气添加量等操作参数来改善气体产物分布、气体热值等；(3) Water vapor is used as the fluidization gas, which is introduced from the bottom of the bubbling fluidized bed to fluidize the oxygen carrier. After the temperature and fluidization of the bed material are stable, the combustible solid waste raw material is fed through the screw After being added to the bed material in the bubbling fluidized bed, the combustible solid waste raw materials will undergo dehydration, pyrolysis, gasification and other reactions rapidly after being heated, and the gas products, tar and fixed carbon will continue to react with the oxygen carrier, making the solid waste gasify further. The gasification products are exported from the top of the bubbling fluidized bed and further utilized after purification. The gas product components can be analyzed through the gas sampling port. According to the analysis results, the gasification temperature, oxygen carrier/combustible solid waste ratio, water vapor addition and other operating parameters can be further adjusted to improve the gas product distribution, gas calorific value, etc. ;
(4)反应后的氧载体通过安装在鼓泡流化床中部的返料管返回流化床提升管。在流化床提升管内，处于还原状态的氧载体被高温空气中的氧气氧化，重新被氧化到氧化状态，回复其晶格氧。氧载体被空气氧化反应是一个强烈的放热反应，通常，根据反应条件可将空气反应器内的反应温度控制在600-950℃范围内；(4) The reacted oxygen carrier returns to the riser of the fluidized bed through the return pipe installed in the middle of the bubbling fluidized bed. In the fluidized bed riser, the oxygen carrier in the reduced state is oxidized by the oxygen in the high-temperature air, and is re-oxidized to the oxidized state to restore its lattice oxygen. The oxidation reaction of oxygen carrier by air is a strong exothermic reaction, usually, the reaction temperature in the air reactor can be controlled within the range of 600-950°C according to the reaction conditions;
(5)产物气体从排气孔流出鼓泡流化床后经旋风分离器分离出固体残渣后通往气体净化装置；重新氧化后的氧载体颗粒被高速空气带出流化床提升管，经旋风分离器分离出气化反应残渣和破损的氧载体碎屑后返回燃料反应器内，继续和可燃固体废弃物发生反应。(5) The product gas flows out of the bubbling fluidized bed from the exhaust hole, and then passes through the cyclone separator to separate the solid residue and then leads to the gas purification device; the re-oxidized oxygen carrier particles are taken out of the fluidized bed riser by high-speed air, and passed through the gas purification device. The cyclone separator separates gasification reaction residues and damaged oxygen carrier debris and returns them to the fuel reactor to continue to react with combustible solid waste.
鼓泡流化床为燃料反应器，流化床提升管为空气反应器。为了保证燃料反应器和空气反应器在反应初期的顺利进行，可以分别在两个反应器的反应段配备外部电加热器。另外，为了防止燃料反应器和空气反应器内的气体相互对流和泄露，在返料管中部设置一个密封室，氧载体颗粒在返回空气反应器过程中，总能充满密封室而起到密封作用。The bubbling fluidized bed is a fuel reactor, and the fluidized bed riser is an air reactor. In order to ensure the smooth progress of the fuel reactor and the air reactor at the initial stage of the reaction, external electric heaters can be equipped in the reaction sections of the two reactors respectively. In addition, in order to prevent the gas in the fuel reactor and the air reactor from convecting and leaking each other, a sealed chamber is set in the middle of the return pipe, and the oxygen carrier particles can always fill the sealed chamber to play a sealing role in the process of returning to the air reactor. .
本发明提出的可燃固体废弃物化学链气化制合成气方法能解决传统可燃固体废弃物气化过程所产生的一系列问题，使可燃固体废弃物在两个串行流化床反应器中高效、经济地转化为优质合成气。本发明采用过渡金属氧化物作为氧载体和燃料反应器中的床料，可燃固体废弃物在燃料反应器中与氧载体发生反应而气化，气化过程所需的氧元素主要由氧载体分子内的晶格氧提供，而不需要额外补充富氧空气作为气化剂，能降低气化成本。被还原后的氧载体返回空气反应器被空气重新氧化，回复晶格氧，然后通过旋风分离器分离灰渣后返回燃料反应器循环使用。如果在燃料反应器中采用水蒸气作为流化气体，则气体产物不被N2和其他惰性气体稀释，能得到高热值的合成气。以过渡金属氧化物为主要组分的氧载体还能对气化过程中产生的焦油和积碳具有催化氧化作用，能降低气化过程中焦油和积碳的产生。The synthesis gas production method of combustible solid waste chemical looping gasification proposed by the present invention can solve a series of problems caused by the traditional combustible solid waste gasification process, and make the combustible solid waste efficient in two serial fluidized bed reactors , Economically converted into high-quality syngas. The present invention adopts transition metal oxide as the bed material in the oxygen carrier and the fuel reactor, and the combustible solid waste reacts with the oxygen carrier in the fuel reactor to be gasified, and the oxygen element required for the gasification process is mainly composed of oxygen carrier molecules The internal lattice oxygen is provided without additional oxygen-enriched air as a gasification agent, which can reduce the cost of gasification. The reduced oxygen carrier is returned to the air reactor to be re-oxidized by air to restore lattice oxygen, and then the ash is separated by the cyclone separator and returned to the fuel reactor for recycling. If water vapor is used as the fluidization gas in the fuel reactor, the gas product will not be diluted by N2 and other inert gases, and high calorific value synthesis gas can be obtained. The oxygen carrier with transition metal oxide as the main component can also catalyze the oxidation of tar and carbon deposits produced in the gasification process, and can reduce the generation of tar and carbon deposits in the gasification process.
本发明是一种突破了现有技术的高效的可燃固体废弃物气化技术，能制取高品质合成气，并能降低气化过程焦油、积碳含量。本发明与现有技术相比具有以下优点：The invention is a high-efficiency combustible solid waste gasification technology that breaks through the prior art, can produce high-quality synthesis gas, and can reduce tar and carbon deposition content in the gasification process. Compared with the prior art, the present invention has the following advantages:
(1)采用氧载体分子中的晶格氧作为可燃固体废弃物气化的氧元素来源，不需要纯氧或富氧空气作为气化剂，只需要少量水蒸气作为流化介质，能降低可燃固体废弃物气化成本；(1) Lattice oxygen in the oxygen carrier molecule is used as the source of oxygen element for the gasification of combustible solid waste. It does not require pure oxygen or oxygen-enriched air as the gasification agent, and only needs a small amount of water vapor as the fluidization medium, which can reduce the flammability Solid waste gasification costs;
(2)由于无需富氧空气作为可燃固体废弃物的气化剂，则所制备的合成气不被N2和未完全反应的过剩O2稀释，提高了合成气的热值；(2) Since there is no need for oxygen-enriched air as a gasification agent for combustible solid waste, the prepared syngas will not be diluted by N2 and incompletely reacted excess O2 , which improves the calorific value of the syngas;
(3)氧载体中的金属氧化物和金属离子对可燃固体废弃物热解过程产生的焦油和积碳能起到催化作用，所以本气化技术能降低可燃固体废弃物气化过程的焦油和积碳产率，提高气化效率；(3) The metal oxides and metal ions in the oxygen carrier can catalyze the tar and carbon deposits produced in the pyrolysis process of combustible solid waste, so this gasification technology can reduce the tar and carbon deposits in the gasification process of combustible solid waste. Carbon deposition yield, improve gasification efficiency;
(4)氧载体颗粒不仅能起到氧载体作用，同时还能起到热载体作用，将空气反应器中放出的反应热带入燃料反应器，节约了能源；氧载体颗粒的存在还改善了燃料反应器内的传热、传质条件，有利于可燃固体废弃物气化反应的顺利进行。(4) Oxygen carrier particles can not only play the role of oxygen carrier, but also play the role of heat carrier, and the reaction heat released in the air reactor is brought into the fuel reactor, saving energy; the existence of oxygen carrier particles also improves the fuel efficiency. The heat transfer and mass transfer conditions in the reactor are conducive to the smooth progress of the combustible solid waste gasification reaction.
附图说明 Description of drawings
附图1为本发明串行流化床反应器结构示意图。Accompanying drawing 1 is the structural diagram of serial fluidized bed reactor of the present invention.
图中，1-螺旋进料器，2-鼓泡流化床(燃料反应器)，3-返料管，4-流化床提升管(空气反应器)，5-旋风分离器，6-旋风分离器Among the figure, 1-screw feeder, 2-bubbling fluidized bed (fuel reactor), 3-return pipe, 4-fluidized bed riser (air reactor), 5-cyclone separator, 6- cyclone separator
具体实施方式 Detailed ways
下面结合实施例进一步说明本发明，但对本发明不构成限制。The present invention is further described below in conjunction with embodiment, but does not constitute limitation to the present invention.
选取农林加工废弃物为生物质原料，平均粒径0.8mm；Fe2O3质量百分含量为60％的三氧化二铁颗粒为氧载体，平均粒径为0.5mm；鼓泡流化床2内径300mm，高1200mm；流化床提升管4直径100mm，高2000mm，初始的氧载体颗粒加入量为30-40kg，根据反应进程可以随时向鼓泡流化床2内补充新鲜氧载体。鼓泡流化床2温度稳定在840-850℃范围内，流化床提升管4温度控制在900-950℃内，制取的合成气由鼓泡流化床2顶部的排气管排出净化后分析、利用。The agricultural and forestry processing waste was selected as the biomass raw material, with an average particle size of 0.8mm; the ferric oxide particles with a mass percentage of Fe 2 O 3 of 60% were used as the oxygen carrier, with an average particle size of 0.5mm; the bubbling fluidized bed 2 The inner diameter is 300mm and the height is 1200mm; the fluidized bed riser 4 has a diameter of 100mm and a height of 2000mm, and the initial amount of oxygen carrier particles added is 30-40kg, and fresh oxygen carriers can be added to the bubbling fluidized bed 2 at any time according to the reaction process. The temperature of the bubbling fluidized bed 2 is stabilized within the range of 840-850°C, the temperature of the fluidized bed riser 4 is controlled within 900-950°C, and the synthesized gas is discharged and purified from the exhaust pipe at the top of the bubbling fluidized bed 2 analysis and utilization.
实施过程如下：将粉碎至0.8mm的生物质原料放置在干燥箱中，在90℃下干燥24小时备用；将35kg氧载体颗粒装载到鼓泡流化床2中，开启鼓泡流化床2和流化床提升管4的外加热电源，将鼓泡流化床2中的氧载体床料加热至850℃；开启蒸汽开关，将水蒸气从鼓泡流化床2底部通入，调节蒸汽流速，使床料能达到鼓泡流化床状态；打开螺旋进料器1，将生物质原料加入到氧载体料床中，与氧载体、水蒸气反应，生物质加入速率为10-12kg/h，产物气体经鼓泡流化床2顶部的排气孔排出，经旋风分离器6分离出气体带出的固体残渣和碎屑，净化后采样分析，然后进一步利用；根据产物气体组分分析判断，当氧载体中的晶格氧快要反应完全的时候，打开返料管3，反应完全的氧载体被气体带入返料管3，进入空气反应器，氧载体被950℃的高温空气氧化，回复到原始的氧化状态，被氧化后的氧载体颗粒，被高速空气带出流化床提升管4，通过旋风分离器5分离出碎屑和残渣，又返回鼓泡流化床2循环使用。The implementation process is as follows: place the biomass raw material crushed to 0.8mm in a drying oven, and dry it at 90°C for 24 hours for later use; load 35kg of oxygen carrier particles into the bubbling fluidized bed 2, and start the bubbling fluidized bed 2 and the external heating power supply of the fluidized bed riser 4 to heat the oxygen carrier bed material in the bubbling fluidized bed 2 to 850°C; turn on the steam switch, and pass water vapor from the bottom of the bubbling fluidized bed 2 to adjust the steam Flow rate, so that the bed material can reach the state of bubbling fluidized bed; open the screw feeder 1, add the biomass raw material into the oxygen carrier material bed, react with the oxygen carrier and water vapor, and the biomass addition rate is 10-12kg/ h, the product gas is discharged through the exhaust hole at the top of the bubbling fluidized bed 2, and the solid residue and debris carried by the gas are separated by the cyclone separator 6, and the sample is analyzed after purification, and then further utilized; according to the analysis of the product gas components Judgment, when the lattice oxygen in the oxygen carrier is about to react completely, open the return pipe 3, the fully reacted oxygen carrier is brought into the return pipe 3 by the gas, enters the air reactor, and the oxygen carrier is oxidized by the high-temperature air at 950°C , return to the original oxidation state, the oxidized oxygen carrier particles are taken out of the fluidized bed riser 4 by the high-speed air, and the debris and residue are separated by the cyclone separator 5, and then returned to the bubbling fluidized bed 2 for recycling .
本实施例原料成分分析如表1所示：Present embodiment raw material component analysis is as shown in table 1:
表1原料成分分析(单位：质量百分含量％)Table 1 raw material composition analysis (unit: mass percentage content %)
本实施例实施结果如下：The implementation result of this embodiment is as follows:
生物质消耗量：10-12kg/hBiomass consumption: 10-12kg/h
平均产气率：1.9m3/kg biomassAverage gas production rate: 1.9m 3 /kg biomass
气体产物主要成分：H2 38.2％，CO 15.7％，CO2 23.5％，CH4 6.6％，CnHm 1.5％，Main components of gas products: H 2 38.2%, CO 15.7%, CO 2 23.5%, CH 4 6.6%, C n H m 1.5%,
合成气热值：14.8MJ/m3 Calorific value of synthesis gas: 14.8MJ/m 3
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