WO2011147180A1

WO2011147180A1 - Biomass combined gasification equipment

Info

Publication number: WO2011147180A1
Application number: PCT/CN2010/080215
Authority: WO
Inventors: 吴创之; 阴秀丽; 周肇秋; 陈坚; 马隆龙
Original assignee: 中国科学院广州能源研究所
Priority date: 2010-05-24
Filing date: 2010-12-24
Publication date: 2011-12-01
Also published as: CN101845328A; CN101845328B

Abstract

A biomass combined gasification equipment comprises a combined gasification furnace. The combined gasification furnace consists of an up-flow section (1), a cross-flow section (7) and a down-flow section (2), of which the insides are communicated in turn. The up-flow section and down-flow section have a circular cross-section and the cross-flow section has a square cross-section. The gas generated by the biomass pyrolyzing and gasifying in the up-flow section of the gasifying furnace tangentially enters the down-flow section of the gasification furnace together with fine solid particles. The up-flow section has a biomass feed inlet (3) and a first gasifying agent inlet (6), the cross-flow section has a second gasifying agent inlet (8), the lower part of the down-flow section has a gas outlet (10), and the bottom of the down-flow section has an ash outlet. The biomass combined gasification equipment combines the processes of pyrolysis, gasification, cracking, reforming and partial oxidation in the same reactor to realize zone-based control and optimization of parameters. The equipment has the characteristics of high gasification efficiency, low tar content, high regulation and control capability for gas components, high load adaptability, strong material applicability, stable running and easy amplification, and can be widely used in the fields of power generation, heat supply, gas supply, liquid fuel synthesis and the like.

Description

一种生物质复合气化装置技术领域 Biomass composite gasification device

本发明涉及生物质气化技术领域，尤其是涉及一种炉内去除焦油的生物质复合气化装置。技术背景 The present invention relates to the field of biomass gasification technology, and more particularly to a biomass composite gasification apparatus for removing tar in a furnace. technical background

由于石油资源的日渐匮乏，环境污染及温室效应问题的日益严重，从丰富的生物质农林废弃物资源（如秸秆等）获取高品位燃料和化学品正逐渐成为一种发展趋势，在国内外引起高度关注。生物质气化技术可将各种废弃的生物质转化成为高品位的气体燃料，用于工业发电、热电联产、集中供气、工业采暖供热，以及作为合成气合成液体燃料以及为燃料电池提供气源等。生物质气化过程由于技术灵活、产物品位高、用途广泛等特点，成为利用低品位生物质中最有前景的技术之一。国内外生物质气化技术已受到广泛重视，相关研究也取得了显著的进展。但目前气化技术仍然存在瓶颈问题，尤其用于低品位生物质时，常规的气化方式不论从焦油含量、气化效率、燃气成分等方面都无法满足需要，因此，迫切需要研究焦油含量低、燃气组份调控能力强以及操作方便的气化工艺，解决目前存在的瓶颈，使生物质气化工艺实现新的突破，在新的应用领域凸显其优势地位。 Due to the depletion of petroleum resources, environmental pollution and the greenhouse effect, the acquisition of high-grade fuels and chemicals from abundant biomass and forestry waste resources (such as straw) is gradually becoming a development trend, causing domestic and foreign highly anticipated. Biomass gasification technology converts a variety of waste biomass into high-grade gaseous fuels for industrial power generation, cogeneration, centralized gas supply, industrial heating, and as a synthetic gas to synthesize liquid fuels and as fuel cells. Provide gas source, etc. Biomass gasification is one of the most promising technologies for the use of low-grade biomass due to its flexible technology, high product quality and versatility. Biomass gasification technology at home and abroad has received extensive attention, and relevant research has also made significant progress. However, there are still bottlenecks in gasification technology. Especially for low-grade biomass, conventional gasification methods cannot meet the needs of tar content, gasification efficiency, gas composition, etc. Therefore, it is urgent to study low tar content. The gasification process with strong gas component regulation ability and convenient operation solves the existing bottlenecks and realizes new breakthroughs in the biomass gasification process, highlighting its dominant position in new application fields.

针对不同的工业用途，国内外对生物质气化技术进行了大量的研究开发工作，开发出固定床、流化床、气流床等不同的生物质气化工艺。不论采用哪种气化工艺，焦油的产生是气化技术的共性问题。焦油在高温时呈气态，与可燃气体完全混合，而在低温时凝结为液态，其分离和处理极为困难。焦油的存在不仅降低了气化效率、气体热值，更严重的是焦油在低温时凝结为液态，容易和水、焦炭、灰等结合，堵塞输气管道，影响气化设备的正常运行；凝结为细小液滴的焦油难以燃烬，在燃烧时容易产生碳黑等颗粒，对燃气设备造成极大的损害。焦油的存在大大降低了合成气的利用价值，阻止了气化技术的高端应用，是气化技术高效大规模应用的瓶颈问题。 For different industrial uses, a large number of research and development work on biomass gasification technology has been carried out at home and abroad, and different biomass gasification processes such as fixed bed, fluidized bed and entrained flow bed have been developed. Regardless of the gasification process used, the generation of tar is a common problem of gasification technology. The tar is in a gaseous state at a high temperature, completely mixed with the combustible gas, and condensed into a liquid state at a low temperature, which is extremely difficult to separate and handle. The presence of tar not only drops Low gasification efficiency, gas calorific value, more serious is that tar condenses into a liquid at low temperature, easily combined with water, coke, ash, etc., blocks the gas pipeline, affects the normal operation of gasification equipment; condenses into fine droplets The tar is difficult to burn, and particles such as carbon black are easily generated during combustion, causing great damage to the gas equipment. The existence of tar greatly reduces the utilization value of syngas, prevents the high-end application of gasification technology, and is the bottleneck problem of efficient and large-scale application of gasification technology.

目前工业上常用的焦油去除方法主要是炉外去除，如干式过滤、湿式洗涤、催化裂解等。过滤和水洗方法虽然操作简单、成本较低，但是效率不高，为防止二次污染，需要增加额外的净化设备和废水处理设备，不仅占地较大，也增加了投资成本，而且处理掉的焦油不能利用，造成能源的浪费。催化裂解***简单、能量利用率高，且对生物质燃气组分具有调变作用而成为国内外研究的热点，但需要消耗大量的额外能量，还需要额外的辅助设备，增加了***的复杂性和投资。同时，由于催化剂失活、机械磨损和应用成本等问题，目前主要用于试验研究，还未形成商业化的专用催化剂系列，尤其在催化剂的使用寿命方面离商业化还存在较大的距离。 At present, the tar removal methods commonly used in the industry are mainly external removal, such as dry filtration, wet washing, catalytic cracking and the like. Although the filtration and water washing methods are simple in operation and low in cost, they are not efficient. In order to prevent secondary pollution, additional purification equipment and wastewater treatment equipment are required, which not only occupies a large area, but also increases investment costs, and is disposed of. Tar can not be used, resulting in waste of energy. Catalytic cracking system is simple, energy utilization is high, and it has a modulation effect on biomass gas components. It has become a hot research topic at home and abroad, but it needs to consume a lot of extra energy. It also needs additional auxiliary equipment, which increases the complexity of the system. And investment. At the same time, due to problems such as catalyst deactivation, mechanical wear and application cost, it is mainly used for experimental research, and a commercialized special catalyst series has not yet been formed, especially in terms of the service life of the catalyst.

焦油也可通过炉内去除的方法即在气化炉内抑制焦油产生并将产生的焦油原位转化为目标产物气，实现气化炉内粗合成气中不含焦油。炉内脱除可以通过优化气化炉结构设计、优化气化过程操作参数、气化炉内添加催化剂等方法实现，从而达到减少气化炉出口燃气中焦油含量的目的。这种方法是目前研究的热点和今后发展方向。 The tar can also be removed in the furnace by suppressing tar production in the gasifier and converting the generated tar into the target product gas in situ, so that the crude syngas in the gasifier does not contain tar. The furnace removal can be achieved by optimizing the structural design of the gasifier, optimizing the operating parameters of the gasification process, adding catalysts in the gasifier, etc., thereby achieving the purpose of reducing the tar content in the gas of the gasifier outlet. This method is the hot spot of research and the future development direction.

国内外气化技术的发展趋势是开发高效、低焦油、燃气组份调控能力较强的气化工艺。针对焦油的有效脱除和燃气的高端利用，国内外开展了新型气化工艺的研究。如：丹麦技术大学设计了两段式气化炉，所得燃气中焦油含量大大降低；德国 Choren公司提出了温和热解和高温热解两步法制高质量合成气的工艺，合成气中几乎不含焦油。这些装置的特点是将诸多的反应器串联在一条连续的流程上，燃料先在间接加热式裂解器中干燥和热解，裂解的产物紧接着在裂解器及焦炭气化器间的狭窄地带进行部分氧化，产物气流经热的焦碳床，从而使产物气中的焦油裂解并达到较低的含量。 The development trend of gasification technology at home and abroad is to develop a gasification process with high efficiency, low tar and gas component control ability. In response to the effective removal of tar and the high-end utilization of gas, research on new gasification processes has been carried out at home and abroad. For example, the Danish Technical University has designed a two-stage gasifier, and the tar content in the obtained gas is greatly reduced; The German company Choren has proposed a two-step high-quality synthesis gas process for mild pyrolysis and high temperature pyrolysis. The synthesis gas contains almost no tar. These devices are characterized by a series of reactors connected in series on a continuous process. The fuel is first dried and pyrolyzed in an indirect heated cracker. The cracked product is then carried out in a narrow zone between the cracker and the coke gasifier. Partial oxidation, the product gas stream passes through a hot coke bed, thereby cracking the tar in the product gas and achieving a lower level.

由上可见，目前炉内脱除焦油的气化工艺多是利用几个反应器的串联实现，只有公开号为 "CN101225315A" 的中国专利提出了一体化的生物质复合气化装置，但由于受到结构空间的限制，颗粒停留时间短，炉内二次反应不充分，组分调变能力不强。发明内容 It can be seen from the above that the gasification process for removing tar in the furnace is mostly realized by the series connection of several reactors. Only the Chinese patent with the publication number "CN101225315A" proposes an integrated biomass composite gasification device, but The limitation of the structural space, the particle residence time is short, the secondary reaction in the furnace is insufficient, and the component modulation ability is not strong. Summary of the invention

本发明提供一种生物质复合气化装置，可将热解、燃烧、气化、焦油裂解、重整和组分调控等反应相对分开，实现参数分区控制和优化匹配，同时所有过程在一套装置中完成，即使不使用催化剂也可达到降低焦油含量、调节气体组分的目的。 The invention provides a biomass composite gasification device, which can separate the reactions of pyrolysis, combustion, gasification, tar cracking, reforming and component regulation, and realize parameter partition control and optimization matching, and all processes are in one set. It is completed in the apparatus, and the purpose of reducing the tar content and adjusting the gas composition can be achieved even without using a catalyst.

为达到以上目的，本发明采取了以下的技术方案： In order to achieve the above object, the present invention adopts the following technical solutions:

本发明装置包括复合气化炉，所述复合气化炉由内部依次连通的气化炉上流段、气化炉横流段和气化炉下流段组成。在所述气化炉上流段设置有生物质进料口和一次气化剂入口；在气化炉横流段上设置有二次气化剂入口；气化炉下流段的下部设置有燃气出口，气化炉下流段底部为灰分分离区，设置有灰分出口。 The apparatus of the present invention comprises a composite gasification furnace comprising an upper part of a gasification furnace in which the interiors are sequentially connected, a cross section of the gasification furnace, and a downstream section of the gasification furnace. a biomass feed inlet and a primary gasification agent inlet are disposed in the upper flow section of the gasification furnace; a secondary gasification agent inlet is disposed on the cross flow section of the gasification furnace; a gas outlet is disposed at a lower portion of the lower flow section of the gasification furnace; The bottom of the downstream section of the gasifier is an ash separation zone, and an ash outlet is provided.

所述气化炉上流段和下流段直径可以相同，下流段高度大于或等于上流段高度的 2/3，上流段和下流段内的流体流动方向相反，上流段截面积和横流段截面积之比大于 10。 The upper and lower flow sections of the gasifier may have the same diameter, the height of the lower flow section is greater than or equal to 2/3 of the height of the upper flow section, and the flow direction of the fluid in the upper flow section and the downstream flow section is opposite, and the cross section of the upper flow section and the cross section of the upper flow section are The area ratio is greater than 10.

所述一次气化剂入口可设置在气化炉上流段的底部，使一次气化剂由气化炉上流段的底部进入气化炉。 The primary gasifying agent inlet may be disposed at the bottom of the upper portion of the gasifier such that the primary gasifying agent enters the gasifier from the bottom of the upper portion of the gasifier.

所述一次气化剂和二次气化剂为空气或氧气或富氧空气，并可根据反应需要加入的水蒸气。所述气化炉上流段和下流段为圆截面，横流段为方形截面，上流段和下流段由横流段切向连接，生物质在气化炉上流段热解气化产生的燃气夹带细小固体颗粒经气化炉横流段切向进入气化炉下流段。由于部分燃气与二次气化剂在横流段发生氧化反应，温度迅速升高，体积迅速膨胀，而且上流段截面积和横流段截面积之比大于 10，所以横流段流速可达到上流段流速的 10倍以上，燃气切向进入下流段时形成高速旋风，有利于燃气混合及固体灰粒分离，同时延长了气化炉下流段的焦油裂解、重整、二次反应时间。 The primary gasifying agent and the secondary gasifying agent are air or oxygen or oxygen-enriched air, and water vapor may be added depending on the reaction. The upper and lower sections of the gasification furnace have a circular cross section, and the cross flow section has a square cross section, and the upper flow section and the lower flow section are tangentially connected by the transverse flow section, and the gas generated by the pyrolysis gasification of the upper stream of the gasification furnace entrains the fine solid. The particles enter the downstream section of the gasifier through the cross section of the gasifier. As part of the gas and the secondary gasification agent oxidize in the cross-flow section, the temperature rises rapidly, the volume expands rapidly, and the ratio of the cross-sectional area of the upstream section to the cross-sectional area of the cross-flow section is greater than 10, so the flow velocity of the cross-flow section can reach the flow velocity of the upper flow section. More than 10 times, the high-speed cyclone is formed when the gas enters the downstream section tangentially, which is beneficial to gas mixing and solid ash separation, and prolongs the tar cracking, reforming and secondary reaction time of the downstream section of the gasifier.

生物质在气化炉上流段内发生热解、气化和生物质焦炭部分燃烧反应，在气化炉横流段内发生生物质燃气部分燃烧反应，在气化炉下流段内发生焦油裂解、重整、二次反应。 Biomass undergoes pyrolysis, gasification and partial combustion of biomass coke in the upper section of the gasifier. Partial combustion reaction of biomass gas occurs in the cross section of the gasifier, and tar cracking occurs in the lower section of the gasifier. Whole and secondary reactions.

在本装置中，气化炉上流段作为生物质热解气化区，温度为 500— 900°C，其中气化炉上流段的中、上部为生物质热解区，温度为 500— 700°C，气化炉上流段的下部为生物质焦炭气化和部分燃烧区，温度 800-900°C ; 气化炉下流段作为焦油裂解、重整、二次反应区为高温区，温度可达到 1000-1300°C ; 气化炉下流段下部燃气出口处的燃气出口管可伸入下流段内约 1/4-1/2气化炉下流段圆截面直径的位置，防止沿下流段壁面下旋分离的固体灰粒进入燃气出口管，下流段的底部为灰分分离区，设置有灰分出口。通过加入不同的气化剂，控制炉内不同区的温度，调节燃气的组分，在一个炉内实现不同工况的控制和优化。本发明生物质复合气化装置将热解、气化、裂解、重整、部分氧化过程在同一反应器内复合，实现参数分区控制和优化。该装置具有气化效率高、焦油含量低、气体组分调控能力强、负荷适应能力强、原料适用性强、运行稳定、易于放大的特点。该装置用于生物质气化可以使燃气中的焦油含量≤20 mg/Nm³，而且运行稳定、连续，可应用于多种领域，如发电、供热、供气、合成液体燃料等。附图说明 In the device, the upper part of the gasifier is used as a biomass pyrolysis gasification zone, and the temperature is 500-900 ° C, wherein the middle and upper parts of the upper section of the gasifier are biomass pyrolysis zones, and the temperature is 500-700°. C. The lower part of the upper part of the gasifier is biomass coke gasification and partial combustion zone, the temperature is 800-900 °C; the lower section of the gasifier is used as the tar cracking, reforming, and the secondary reaction zone is the high temperature zone, and the temperature can reach 1000-1300°C; the gas outlet pipe at the lower gas outlet of the lower part of the gasification furnace can extend into the downstream section of the downstream section of the 1/4-1/2 gasifier with a circular cross-sectional diameter to prevent the lower section of the downstream section. The spin-separated solid ash particles enter the gas outlet pipe, and the bottom of the downstream section is an ash separation zone, and an ash outlet is provided. By adding different gasifying agents, controlling the temperature in different zones of the furnace, adjusting the composition of the gas, and controlling and optimizing different working conditions in one furnace. The biomass composite gasification device of the invention combines pyrolysis, gasification, cracking, reforming and partial oxidation processes in the same reactor to realize parameter partition control and optimization. The device has the characteristics of high gasification efficiency, low tar content, strong gas component regulation ability, strong load adaptability, strong material suitability, stable operation and easy amplification. The device is used for biomass gasification to make the tar content in the gas ≤ 20 mg/Nm ³ , and the operation is stable and continuous, and can be applied to various fields such as power generation, heat supply, gas supply, and synthetic liquid fuel. DRAWINGS

图 1为本发明装置实施例结构示意图（正视图）； Figure 1 is a schematic structural view of a device embodiment of the present invention (front view);

图 2为图 1的俯视结构示意图。 Figure 2 is a schematic plan view of the structure of Figure 1.

附图标记说明： Description of the reference signs:

1.气化炉上流段 2. 气化炉下流段 3. 生物质进料口 4.生物质热解区 5.焦炭气化和部分燃烧区 6.—次气化剂入口 7.气化炉横流段 8.二次气化剂入口 9.灰分分离区 10.燃气出口具体实施方式 1. Gasifier upflow section 2. Gasifier downflow section 3. Biomass feed port 4. Biomass pyrolysis zone 5. Coke gasification and partial combustion zone 6. Secondary gasification agent inlet 7. Gasifier Crossflow section 8. Secondary gasification agent inlet 9. Ash separation zone 10. Gas outlet embodiment

下面结合附图与具体实施方式对本发明内容做进一步的说明。 The content of the present invention will be further described below in conjunction with the drawings and specific embodiments.

如图 1、 2所示，本发明装置包括复合气化炉，所述复合气化炉由内部依次连通的气化炉上流段 1、气化炉横流段 7和气化炉下流段 2组成。在气化炉上流段 1设置有生物质进料口 3，底部设置有一次气化剂入口 6; 气化炉上流段 1的中、上部为生物质热解区 4，下部为焦炭气化和部分燃烧区 5。气化炉上流段和下流段为圆截面，气化炉上流段 1和气化炉下流段 2的直径可以相同，下流段高度大于或等于上流段高度的 2/3，气化炉横流段 7为方形截面，上流段 1的截面积和横流段 Ί的截面积之比大于 10，生物质在气化炉上流段 1热解气化产生的燃气夹带细小固体颗粒经气化炉横流段 7切向进入气化炉下流段 2。在所述气化炉横流段 7入口设置有二次气化剂入口 8。气化炉下流段 2的下部设置有燃气出口 10，燃气出口管伸入下流段内约 1/4-1/2气化炉下流段圆截面直径的位置，底部为灰分分离区 9，设置有灰分出口。 As shown in Figs. 1 and 2, the apparatus of the present invention comprises a composite gasification furnace comprising an upper part of a gasification furnace, a cross section 7 of a gasification furnace, and a downstream section 2 of a gasification furnace which are sequentially connected in series. In the gasifier upper flow section 1 is provided with a biomass feed port 3, and at the bottom is provided a primary gasification agent inlet 6; the middle and upper parts of the gasifier upper flow section 1 are biomass pyrolysis zone 4, and the lower part is coke gasification and Partial combustion zone 5. The upper section and the lower section of the gasification furnace have a circular cross section, and the diameter of the upper section of the gasifier and the downstream section of the gasifier can be the same, the height of the downstream section is greater than or equal to 2/3 of the height of the upper section, and the cross section of the gasifier is 7 Square section, section of the upper section 1 The ratio of the cross-sectional area of the product and the cross-flow section 大于 is greater than 10, and the gas-entrained fine solid particles generated by the pyrolysis gasification of the biomass in the upper section of the gasifier are tangentially introduced into the downstream section 2 of the gasifier through the cross-flow section 7 of the gasifier. A secondary gasification agent inlet 8 is provided at the inlet of the gasifier cross section 7. The gas outlet 10 is disposed at a lower portion of the downstream section 2 of the gasifier, and the gas outlet pipe extends into a position of a circular cross-sectional diameter of a downstream section of the 1/4-1/2 gasifier in the downstream section, and the bottom is an ash separation zone 9 provided with Ash outlet.

实施例 1 : Example 1

生物质木屑从进料口 3加入复合气化炉上流段 1内的热解区 4，在 500-700°C 温度下发生热解反应，生物质释放出挥发气体，并生成固体焦炭；焦炭大颗粒向下流入气化炉上流段 1内的焦炭气化和部分燃烧区 5，在一次气化剂入口 6加入的富氧空气（0₂浓度 90%) 的作用下，少部分焦炭发生氧化反应，使焦炭气化和部分燃烧区 5温度达到 800-900°C，大部分焦炭则发生气化反应生成可燃气体；自焦炭气化和部分燃烧区 5向上流动的高温气体为生物质热解区 4提供生物质热解所需的热量，维持热解区 4的温度在 500-700°C ; 生物质在气化炉上流段 1内反应产生的气体夹带细小固体颗粒经气化炉横流段 7 切向进入气化炉下流段 2 内。从二次气化剂进气口 8加入适量二次富氧空气，使部分可燃气体发生氧化反应，温度迅速升高，体积迅速膨胀，而且由于上流段 1的截面积和横流段 7的截面积之比大于 10，所以横流段 7的流速可达到上流段 1的流速的 10倍以上，燃气切向进入下流段 2 时形成高速旋风。气化炉下流段 2 内的局部温度可达到 1200°C左右，焦油在此高温条件下发生裂解反应转化成可燃气体，同时燃气夹带的颗粒中的残碳还可通过二次反应转化成可燃气体；在燃气切向高速旋转进入气化炉下流段 2的过程中，其携带的固体灰粒在离心力作用下从气体中分离出来向下流入气化炉下流段 2的下部连接的灰分分离区 9，可燃气体则从气化炉下流段 2下部的燃气出口 10进入下游装置。富氧空气当量比 ER=0.21-0.29时，得到的燃气成分为 H₂ 21.4%-25.4%, N₂ 2.9%-3.8%, CO 38.8%-45.2%, CH₄ 4.9%-7.0%, C0₂ 18.5%-25.1%, 气化效率 74.9%-85.0%，碳转化率 91.8%-99.6%。在气化炉下流段 2内没有通入二次富氧空气气化剂的情况下，燃气出口 10可燃气体中焦油的含量为 900 mg/m³; 当通入二次富氧空气气化剂时，焦油在高温区发生裂解反应，燃气出口 10的可燃气体中焦油的含量降至 20 mg/m³以下。焦油裂解后燃气中各组分的含量无明显变化，因为焦油裂解除 N₂外其他气体都有产生，但焦油裂解成可燃气体使生物质产气率由 1.07 Nm³/kg提高到 1.21 Nm³/kg。 The biomass wood chips are fed from the feed port 3 to the pyrolysis zone 4 in the upper stream section 1 of the composite gasification furnace, and a pyrolysis reaction occurs at a temperature of 500-700 ° C, and the biomass releases volatile gas and generates solid coke; The particles flow downward into the coke gasification and partial combustion zone 5 in the upper section 1 of the gasifier. Under the action of the oxygen-enriched air (0 ₂ concentration 90%) added by the primary gasifier inlet 6, a small portion of the coke undergoes an oxidation reaction. , the coke gasification and partial combustion zone 5 temperature reaches 800-900 ° C, most of the coke gasification reaction to generate combustible gas; from the coke gasification and partial combustion zone 5 upward flow of high temperature gas is the biomass pyrolysis zone 4 Providing the heat required for biomass pyrolysis, maintaining the temperature of the pyrolysis zone 4 at 500-700 ° C; the gas produced by the reaction of the biomass in the upper section of the gasifier is entrained with fine solid particles through the cross section of the gasifier 7 Tangentially enters the lower section 2 of the gasifier. An appropriate amount of secondary oxygen-enriched air is added from the secondary gasification agent inlet 8 to cause oxidation of a part of the combustible gas, the temperature is rapidly increased, the volume is rapidly expanded, and the cross-sectional area of the upstream section 1 and the cross-sectional area of the cross-flow section 7 The ratio is greater than 10, so the flow velocity of the lateral flow section 7 can reach 10 times or more of the flow velocity of the upper flow section 1, and the high-speed cyclone is formed when the gas tangentially enters the downstream flow section 2. The local temperature in the downstream section 2 of the gasifier can reach about 1200 °C, and the tar is converted into a combustible gas by the cracking reaction under the high temperature condition, and the residual carbon in the gas entrained particles can also be converted into the combustible gas by the secondary reaction. During the tangential rotation of the gas into the lower section 2 of the gasifier, the solid ash carried by the gas is separated from the gas by centrifugal force and flows down into the ash separation zone connected to the lower part of the downstream section 2 of the gasifier 9 , the combustible gas is from the downstream section of the gasifier 2 The lower gas outlet 10 enters the downstream unit. When the oxygen-enriched air equivalent ratio ER=0.21-0.29, the gas composition obtained is H ₂ 21.4%-25.4%, N ₂ 2.9%-3.8%, CO 38.8%-45.2%, CH ₄ 4.9%-7.0%, C0 ₂ 18.5%-25.1%, gasification efficiency 74.9%-85.0%, carbon conversion rate 91.8%-99.6%. In the case where no secondary oxygen-enriched air gasifying agent is introduced into the downstream section 2 of the gasifier, the content of tar in the combustible gas of the gas outlet 10 is 900 mg/m ³ ; when the secondary oxygen-enriched air gasifying agent is introduced At the time, the tar is cracked in the high temperature zone, and the tar content in the combustible gas of the gas outlet 10 is reduced to 20 mg/m ³ or less. After the tar cracking, the content of each component in the gas did not change significantly, because the tar cracking occurred except for N ₂ , but the tar cracked into a combustible gas to increase the biomass gas production rate from 1.07 Nm ³ /kg to 1.21 Nm ^{3 .} /kg.

实施例 2: Example 2:

生物质木屑从进料口 3加入复合气化炉上流段 1内的热解区 4，在 500-700°C 温度下发生热解反应，生物质释放出挥发气体，并生成固体焦炭；焦炭大颗粒向下流入气化炉上流段 1内的焦炭气化和部分燃烧区 5，在从一次气化剂入口 6加入的富氧空气（0₂浓度 90%) 的作用下，少部分焦炭发生氧化反应，使焦炭气化和部分燃烧区 5温度达到 800-900°C，大部分焦炭则发生气化反应生成可燃气体；自焦炭气化和部分燃烧区 5向上流动的高温气体为生物质热解区 4提供生物质热解所需的热量，维持热解区 4的温度在 500-700°C ; 生物质在气化炉上流段 1内反应产生的气体夹带细小固体颗粒经气化炉横流段 7切向进入气化炉下流段 2内。从二次气化剂进气口 8加入适量二次富氧空气，使部分可燃气体发生氧化反应，温度迅速升高，体积迅速膨胀，而且由于上流段 1的截面积和横流段 7的截面积之比大于 10，所以横流段 7的流速可达到上流段 1的流速的 10倍以上，燃气切向进入下流段 2时形成高速旋风。为提高燃气出口 10可燃气体中 H₂/CO 比，即提高 H₂含量，降低 CO含量，提高合成气质量，在二次气化剂中加入水蒸气，通过水气变换反应 CO+H₂0→C0₂+H₂以及水蒸气重整反应，对气体组分进行调控。在二次气化剂反应条件下气化炉下流段 2内的局部温度可达到 1100°C 左右，焦油在此高温条件下发生裂解反应转化成可燃气体，水汽变换反应使燃气中的 H₂和 CO组分受到定向调控；同时燃气夹带的粒中的残碳还可通过二次反应转化成可燃气体；在燃气切向高速旋转进入气化炉下流段 2的过程中，其携带的固体灰粒在离心力作用下从气体中分离出来向下流入气化炉下流段 2 的下部连接的灰分分离区 9，可燃气体则从气化炉下流段 2下部的燃气出口 10进入下游装置。在富氧空气当量比 ER=0.26情况下，当水蒸气 /生物质原料比（质量） S/B=0.1-0.5 时，得到的燃气成分为 H₂ 24.6%-28.7%, N₂ 2.8%-3.8%, CO 27.1%-33.8%, CH₄ 3.9%-4.1%, C0₂ 29.3%-32.7%, 气化效率 73.9%-78%, 碳转化率 97.5%-98.4%。与实施例 1比较可知，通过添加水蒸气使 H₂/CO平均值由 0.56 提高到 0.88，最高已达到 1.0以上，有利于后续的合成反应应用，但是 C0₂含量增加，合成前需要进行脱除。 The biomass wood chips are fed from the feed port 3 to the pyrolysis zone 4 in the upper stream section 1 of the composite gasification furnace, and a pyrolysis reaction occurs at a temperature of 500-700 ° C, and the biomass releases volatile gas and generates solid coke; particles flowing down into the upstream section of the gasification furnace 1 and the char in the gasification portion of the combustion zone 5, under the action of a gasifying agent inlet 6 from the addition of oxygen enriched air (0 ₂ concentration of 90%), a small portion of the oxidation of coke The reaction, the coke gasification and the partial combustion zone 5 temperature reaches 800-900 ° C, most of the coke gasification reaction generates flammable gas; the high temperature gas flowing from the coke gasification and partial combustion zone 5 is biomass pyrolysis Zone 4 provides the heat required for biomass pyrolysis, maintaining the temperature of the pyrolysis zone 4 at 500-700 ° C; the gas produced by the reaction of biomass in the upper section of the gasifier is entrained with fine solid particles through the cross section of the gasifier 7 tangentially enters the lower section 2 of the gasifier. An appropriate amount of secondary oxygen-enriched air is added from the secondary gasification agent inlet 8 to cause oxidation of a part of the combustible gas, the temperature is rapidly increased, the volume is rapidly expanded, and the cross-sectional area of the upstream section 1 and the cross-sectional area of the cross-flow section 7 The ratio is greater than 10, so the flow velocity of the cross flow section 7 can reach 10 times or more of the flow velocity of the upper flow section 1, and the high-speed cyclone is formed when the gas tangentially enters the downstream flow section 2. In order to increase the H ₂ /CO ratio in the flammable gas of the gas outlet 10, that is, increase the H ₂ content, reduce the CO content, increase the quality of the synthesis gas, and add water to the secondary gasification agent. The vapor is regulated by a water gas shift reaction CO + H ₂ 0 → C0 ₂ + H ₂ and a steam reforming reaction. Under the condition of the secondary gasification agent, the local temperature in the lower stream section 2 of the gasifier can reach about 1100 ° C. The tar is cracked into a combustible gas under the high temperature condition, and the water vapor shift reaction makes the H ₂ in the gas. The CO component is subject to directional regulation; at the same time, the residual carbon in the gas entrained granules can also be converted into flammable gas by the secondary reaction; the solid ash particles carried during the tangential rotation of the gas into the lower stream section 2 of the gasifier The gas is separated from the gas and flows downward into the ash separation zone 9 connected to the lower portion of the downstream section 2 of the gasifier, and the combustible gas enters the downstream device from the gas outlet 10 at the lower portion of the downstream section 2 of the gasifier. In the case of oxygen-enriched air equivalent ratio ER=0.26, when the steam/biomass raw material ratio (mass) S/B=0.1-0.5, the obtained gas composition is H ₂ 24.6%-28.7%, N ₂ 2.8%- 3.8%, CO 27.1%-33.8%, CH ₄ 3.9%-4.1%, C0 ₂ 29.3%-32.7%, gasification efficiency 73.9%-78%, carbon conversion 97.5%-98.4%. Compared with Example 1, it can be seen that the average value of H ₂ /CO is increased from 0.56 to 0.88 by adding steam, and the highest has reached 1.0 or more, which is beneficial to the subsequent synthesis reaction application, but the content of C0 _{2 is} increased, and removal is required before synthesis. .

Claims

权利要求 Rights request

1、一种生物质复合气化装置，包括复合气化炉，其特征在于：所述复合气化炉由内部依次连通的气化炉上流段、气化炉横流段和气化炉下流段组成；在所述气化炉上流段设置有生物质进料口和一次气化剂入口；在气化炉横流段上设置有二次气化剂入口；气化炉下流段的下部设置有燃气出口，气化炉下流段底部为灰分分离区，设置有灰分出口；所述气化炉上流段作为生物质热解气化区，温度为 500— 900°C，其中气化炉上流段的中、上部为生物质热解区，温度为 500— 700°C，气化炉上流段的下部为生物质焦炭气化和部分燃烧区，温度 800-90CTC ; 气化炉下流段作为焦油裂解、重整、二次反应区，温度可达到 1000-130CTC ; 所述气化炉上流段和下流段为圆截面，横流段为方形截面，上流段和下流段由横流段切向连接，生物质在气化炉上流段热解气化产生的燃气夹带细小固体颗粒经气化炉横流段切向进入气化炉下流段。 A biomass composite gasification device, comprising a composite gasification furnace, characterized in that: the composite gasification furnace is composed of an upper gasification furnace section, a gasification furnace crossflow section and a gasification furnace downstream section which are sequentially connected internally; a biomass feed inlet and a primary gasification agent inlet are disposed in the upper flow section of the gasification furnace; a secondary gasification agent inlet is disposed on the cross flow section of the gasification furnace; a gas outlet is disposed at a lower portion of the lower flow section of the gasification furnace; The bottom part of the lower part of the gasifier is an ash separation zone, and an ash outlet is arranged; the upper section of the gasifier is used as a biomass pyrolysis gasification zone, and the temperature is 500-900 ° C, wherein the middle and upper parts of the upper section of the gasifier For the biomass pyrolysis zone, the temperature is 500-700 °C, the lower part of the upper part of the gasifier is biomass coke gasification and partial combustion zone, the temperature is 800-90 CTC; the lower section of the gasifier is used for tar cracking, reforming, In the secondary reaction zone, the temperature can reach 1000-130 CTC; the upper and lower sections of the gasification furnace have a circular cross section, the transverse flow section is a square cross section, and the upper flow section and the lower flow section are tangentially connected by the transverse flow section, and the biomass is in the gasification furnace. Upper section heat Gas produced by gasification of solid fine particles are entrained flow gasifier cross-section of the gasifier tangentially into the downstream segment.

2、如权利要求 1所述的生物质复合气化装置，其特征在于，所述气化炉上流段和气化炉下流段的直径相同，下流段高度大于或等于上流段高度的 2/3; 所述上流段截面积和横流段截面积之比大于 10。 2 . The biomass composite gasification apparatus according to claim 1 , wherein the gasifier upper flow section and the gasifier lower flow section have the same diameter, and the lower flow section height is greater than or equal to 2/3 of the height of the upper flow section; The ratio of the cross-sectional area of the upflow section to the cross-sectional area of the crossflow section is greater than 10.

3、如权利要求 1所述的生物质复合气化装置，其特征在于，所述燃气出口管伸入气化炉下流段内 1/4-1/2气化炉下流段圆截面直径的位置。 3. The biomass composite gasification apparatus according to claim 1, wherein the gas outlet pipe extends into a circular section diameter of a lower section of the 1/4-1/2 gasification furnace in the downstream section of the gasification furnace. .

4、如权利要求 1所述的生物质复合气化装置，其特征在于，所述二次气化剂入口设置在横流段入口。 The biomass composite gasification apparatus according to claim 1, wherein the secondary gasification agent inlet is provided at the inlet of the cross flow section.

5、如权利要求 1所述的生物质复合气化装置，其特征在于，所述一次气化剂和二次气化剂为空气或氧气或富氧空气。 The biomass composite gasification apparatus according to claim 1, wherein the primary gasifying agent and the secondary gasifying agent are air or oxygen or oxygen-enriched air.

6、如权利要求 5所述的生物质复合气化装置，其特征在于，所述一次气化剂和二次气化剂中根据反应需要可添加水蒸气。 The biomass composite gasification apparatus according to claim 5, wherein the primary gasifying agent and Water vapor may be added to the secondary gasifying agent depending on the reaction needs.