CN103146432A - Biomass pyrolysis gasification and tar catalytic cracking device and method - Google Patents
Biomass pyrolysis gasification and tar catalytic cracking device and method Download PDFInfo
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 61
- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title claims abstract description 21
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Abstract
一种生物质热解气化与焦油催化裂解的装置与方法属于生物质能利用技术领域。该装置包括料斗、进料系统、生物质热解气化系统、焦油催化裂解系统、流化床焦炭燃烧系统、热砂子分离系统、流化床催化剂再生系统、催化剂分离系统；其中生物质热解气化系统包含多个旋风反应分离器，用于生物质原料在气化介质下的高效气化反应获得富氢合成气，并使生物质原料充分反应；另外，焦油催化裂解系统包含多个旋风反应分离器，用于焦油的高效催化裂解，使焦油充分反应从而获得极低焦油含量的富氢合成气，并使失活催化剂及时排出催化反应系统。该装置通过引入多级旋风反应分离器，可实现生物质高效气化以及焦油的高效转化，从而获得低级焦油含量的富氢合成气。
A device and method for biomass pyrolysis gasification and tar catalytic cracking belong to the technical field of biomass energy utilization. The device includes a hopper, a feed system, a biomass pyrolysis gasification system, a tar catalytic cracking system, a fluidized bed coke combustion system, a hot sand separation system, a fluidized bed catalyst regeneration system, and a catalyst separation system; The gasification system includes multiple cyclone reaction separators, which are used for the efficient gasification reaction of biomass raw materials in the gasification medium to obtain hydrogen-rich synthesis gas and fully react the biomass raw materials; in addition, the tar catalytic cracking system includes multiple cyclone The reaction separator is used for high-efficiency catalytic cracking of tar, so that tar can be fully reacted to obtain hydrogen-rich synthesis gas with extremely low tar content, and the deactivated catalyst can be discharged from the catalytic reaction system in time. By introducing a multi-stage cyclone reaction separator, the device can realize high-efficiency gasification of biomass and high-efficiency conversion of tar, thereby obtaining hydrogen-rich synthesis gas with low-grade tar content.
Description
技术领域 technical field
本发明属于生物质能的高效利用技术领域，具体涉及一种生物质热解气化与焦油催化裂解的装置与方法。The invention belongs to the technical field of high-efficiency utilization of biomass energy, and in particular relates to a device and method for pyrolysis gasification of biomass and catalytic cracking of tar.
背景技术 Background technique
随着化石资源的日益枯竭，生物质资源的开发利用获得了全球的广泛关注。在众多的生物质转化利用技术中，气化是一种非常重要的技术；根据使用气化介质、反应工况、反应装置等的不同，生物质气化有多种不同的形式，并可获得不同的气化产物分布。现阶段，生物质常规气化技术（空气气化）已经发展较为成熟，但在工业化应用过程中面临着一大技术瓶颈——焦油的处理。生物质气化过程中不可避免会产生焦油，焦油的存在具有多种不利影响：（1）焦油占可燃气能量的5%～10%，在低温下难以与可燃气一起被燃烧利用，因此大部分焦油的能量被浪费掉；（2）焦油在低温下冷凝成粘稠状液体，容易和水、炭粒等结合在一起，堵塞输气管道，卡住阀门、抽风机转子，腐蚀金属；（3）焦油难以完全燃烧，并产生炭黑等颗粒，对燃气利用设备如内燃机、燃气轮机等损害相当严重；（4）焦油及其燃烧后产生的气味对人体是有害的。因此，如何实现焦油的高效转化是生物质气化技术大规模应用必须解决的关键技术难题。现阶段，催化裂解是实现焦油高效转化的最有效技术途径，其工业实施的关键技术包括催化剂的选择以及催化反应设备的开发。With the depletion of fossil resources, the development and utilization of biomass resources has received widespread attention worldwide. Among many biomass conversion and utilization technologies, gasification is a very important technology; depending on the use of gasification media, reaction conditions, reaction devices, etc., there are many different forms of biomass gasification, and can be obtained Different distribution of gasification products. At this stage, conventional biomass gasification technology (air gasification) has been developed relatively maturely, but it faces a major technical bottleneck in the process of industrial application—the treatment of tar. Tar is inevitably produced during the biomass gasification process. The existence of tar has many adverse effects: (1) Tar accounts for 5% to 10% of the energy of combustible gas, and it is difficult to be burned and utilized together with combustible gas at low temperature, so it Part of the energy of the tar is wasted; (2) The tar condenses into a viscous liquid at low temperature, which is easy to combine with water and carbon particles to block the gas pipeline, block the valve, the exhaust fan rotor, and corrode the metal; ( 3) Tar is difficult to burn completely and produces particles such as carbon black, which seriously damages gas utilization equipment such as internal combustion engines and gas turbines; (4) Tar and the smell it produces after burning are harmful to the human body. Therefore, how to realize the efficient conversion of tar is a key technical problem that must be solved for the large-scale application of biomass gasification technology. At present, catalytic cracking is the most effective technical way to achieve high-efficiency conversion of tar, and the key technologies for its industrial implementation include the selection of catalysts and the development of catalytic reaction equipment.
除了常规的空气气化技术以外，以水蒸气、CO2、气化混合气等为气化介质的生物质气化技术也获得了较多的关注；然而，这些气化技术在工业应用中存在的一个重要问题是生物质与气化介质的反应相对较为缓慢，使得生物质在有限的反应器空间以及反应时间内难以充分反应；因此如何实现生物质在特定气化介质下的高效气化反应是目前亟待解决的另一个重要技术问题。In addition to the conventional air gasification technology, the biomass gasification technology using water vapor, CO 2 , gasification gas mixture, etc. as the gasification medium has also received more attention; An important issue is that the reaction between biomass and gasification medium is relatively slow, making it difficult for biomass to fully react within the limited reactor space and reaction time; therefore, how to achieve efficient gasification reaction of biomass in a specific gasification medium It is another important technical problem to be solved urgently at present.
发明内容 Contents of the invention
本发明的目的在于克服现有技术的不足，提供一种生物质热解气化与焦油催化裂解的装置与方法。The purpose of the present invention is to overcome the deficiencies of the prior art and provide a device and method for pyrolysis gasification of biomass and catalytic cracking of tar.
本发明所述的生物质热解气化与焦油催化裂解装置采用的技术方案为：The technical scheme adopted by the biomass pyrolysis gasification and tar catalytic cracking device of the present invention is:
该装置包括料斗、进料系统、生物质热解气化系统、焦油催化裂解系统、流化床焦炭燃烧系统、热砂子分离系统、流化床催化剂再生系统、催化剂分离系统：The device includes a hopper, a feed system, a biomass pyrolysis gasification system, a tar catalytic cracking system, a fluidized bed coke combustion system, a hot sand separation system, a fluidized bed catalyst regeneration system, and a catalyst separation system:
所述料斗的出口与进料系统的入口相连；流化床焦炭燃烧系统的底部与鼓风机相连，直接供入过量空气，其侧壁下端还有一个入口用于补充新砂子；热砂子分离系统包括两级旋风分离器，其中第一级旋风分离器的进口与流化床焦炭燃烧系统的出口相连，排气口与第二级旋风分离器的进口相连，第二级旋风分离器的出气口与流化床催化剂再生系统的底部气体入口相连，排料口与集灰箱相连，直接收集飞灰；流化床催化剂再生系统的侧壁下端设有一个入口用于补充新催化剂；催化剂分离系统为单级旋风分离器，其进口与流化床催化剂再生系统的出口相连；The outlet of the hopper is connected with the inlet of the feeding system; the bottom of the fluidized bed coke combustion system is connected with the blower to directly supply excess air, and there is an inlet at the lower end of the side wall for replenishing new sand; the hot sand separation system includes Two-stage cyclone separator, wherein the inlet of the first-stage cyclone separator is connected to the outlet of the fluidized bed coke combustion system, the exhaust port is connected to the inlet of the second-stage cyclone separator, and the gas outlet of the second-stage cyclone separator is connected to the outlet of the fluidized bed coke combustion system. The bottom gas inlet of the fluidized bed catalyst regeneration system is connected, and the discharge port is connected with the ash collection box to directly collect fly ash; the lower end of the side wall of the fluidized bed catalyst regeneration system is provided with an inlet for replenishing new catalyst; the catalyst separation system is A single-stage cyclone separator, the inlet of which is connected with the outlet of the fluidized bed catalyst regeneration system;
所述生物质热解气化系统包括多个旋风反应分离器；所述的多个旋风反应分离器自上而下串联，定义最上面的旋风反应分离器为旋风反应分离器第一组第一单元，向下依次为旋风反应分离器第一组第二单元，······，旋风反应分离器第一组最末单元，其中，N为不小于2的整数；The biomass pyrolysis gasification system includes a plurality of cyclone reaction separators; the plurality of cyclone reaction separators are connected in series from top to bottom, and the uppermost cyclone reaction separator is defined as the first group of cyclone reaction separators. Units, down to the second unit of the first group of cyclone reaction separator, ..., the last unit of the first group of cyclone reaction separator, wherein, N is an integer not less than 2;
所述焦油催化裂解系统包括多个旋风反应分离器；所述的多个旋风反应分离器自下而上串联，定义最下面的旋风反应分离器为旋风反应分离器第二组第一单元，向上依次为旋风反应分离器第二组第二单元，······，旋风反应分离器第二组最末单元，其中，n为不小于2的整数；The tar catalytic cracking system includes a plurality of cyclone reaction separators; the plurality of cyclone reaction separators are connected in series from bottom to top, and the bottom cyclone reaction separator is defined as the first unit of the second group of cyclone reaction separators. In turn, the second unit of the second group of cyclone reaction separator, ..., the last unit of the second group of cyclone reaction separator, wherein, n is an integer not less than 2;
所述旋风反应分离器第一组第一单元的排料口与旋风反应分离器第一组第二单元的进料口相连，旋风反应分离器第一组第二单元的排气口与旋风反应分离器第一组第一单元的进气口相连；旋风反应分离器第一组第二单元的排料口与旋风反应分离器第一组第三单元的进料口相连，旋风反应分离器第一组第三单元的排气口与旋风反应分离器第一组第二单元的进气口相连，依次类推至旋风反应分离器第一组最末单元；其中，旋风反应分离器第一组第一单元的侧部还有两个进料口，其中一个进料口与进料系统的出口相连，另一个进料口与热砂子分离系统中第一级旋风分离器的排料口相连，旋风反应分离器第一组第一单元的排气口与焦油催化裂解系统中旋风反应分离器第二组第一单元的进气口相连；旋风反应分离器第一组最末单元的排料口和进气口分别与流化床焦炭燃烧系统的侧壁下端开口、旋风反应分离器第二组最末单位的出气口相连；The discharge port of the first group of the first unit of the cyclone reaction separator is connected with the feed port of the first group of the second unit of the cyclone reaction separator, and the exhaust port of the first group of the second unit of the cyclone reaction separator is connected with the cyclone reaction separator. The air inlet of the first unit of the first group of the separator is connected; the discharge port of the second unit of the first group of the cyclone reaction separator is connected with the feed port of the third unit of the first group of the cyclone reaction separator, and the first group of the cyclone reaction separator is connected to the inlet of the third unit. The exhaust port of the third unit of the first group is connected with the air inlet of the second unit of the first group of the cyclone reaction separator, and so on to the last unit of the first group of the cyclone reaction separator; wherein, the first group of the cyclone reaction separator There are two feed ports on the side of the first unit, one of which is connected to the outlet of the feed system, and the other feed port is connected to the discharge port of the first-stage cyclone separator in the hot sand separation system. The exhaust port of the first unit of the first group of reaction separator is connected with the inlet port of the first unit of the second group of cyclone reaction separator in the tar catalytic cracking system; the discharge port of the last unit of the first group of cyclone reaction separator and The air inlet is respectively connected with the opening at the lower end of the side wall of the fluidized bed coke combustion system and the gas outlet of the second group of the last unit of the cyclone reaction separator;
旋风反应分离器第二组第一单元的排气口与旋风反应分离器第二组第二单元的进气口相连，旋风反应分离器第二组第二单元的排料口与旋风反应分离器第二组第一单元的进料口相连；旋风反应分离器第二组第二单元的排气口与旋风反应分离器第二组第三单元的进气口相连，旋风反应分离器第二组第三单元的排料口与旋风反应分离器第二组第二单元的进料口相连，依次类推至旋风反应分离器第二组最末单元；其中，旋风反应分离器第二组第一单元的进气口和排料口分别与生物质热解气化系统中旋风反应分离器第一组第一单元的排气口和流化床催化剂再生系统的侧壁下端开口相连；旋风反应分离器第二组最末单元的进料口与催化剂分离系统的排料口相连，旋风反应分离器第二组最末单元的排气口分为两路，一路与生物质热解气化系统中旋风反应分离器第一组最末单元的进气口相连，另一路直接收集极低焦油含量的富氢合成气。The exhaust port of the second group of the first unit of the cyclone reaction separator is connected with the inlet port of the second group of the second unit of the cyclone reaction separator, and the discharge port of the second group of the second unit of the cyclone reaction separator is connected with the cyclone reaction separator The feed port of the first unit of the second group is connected; the exhaust port of the second unit of the second group of the cyclone reaction separator is connected with the inlet of the third unit of the second group of the cyclone reaction separator, and the second group of the cyclone reaction separator The discharge port of the third unit is connected to the feed port of the second group of the second unit of the cyclone reaction separator, and so on to the last unit of the second group of the cyclone reaction separator; wherein, the first unit of the second group of the cyclone reaction separator The air inlet and discharge port of the biomass pyrolysis gasification system are respectively connected with the exhaust port of the first group of the first unit of the cyclone reaction separator in the biomass pyrolysis gasification system and the lower end opening of the side wall of the fluidized bed catalyst regeneration system; the cyclone reaction separator The feed port of the final unit of the second group is connected to the discharge port of the catalyst separation system, and the exhaust port of the final unit of the second group of the cyclone reaction separator is divided into two routes, one of which is connected with the cyclone in the biomass pyrolysis gasification system. The air inlets of the last unit of the first group of reaction separators are connected, and the other one directly collects the hydrogen-rich synthesis gas with extremely low tar content.
所述进料系统为螺旋进料器。The feeding system is a screw feeder.
一种基于所述装置的生物质热解气化与焦油催化裂解方法，具有以下步骤：A biomass pyrolysis gasification and tar catalytic cracking method based on the device has the following steps:
将生物质原料经料斗和进料系统送入生物质热解气化系统的旋风反应分离器第一组第一单元；同时，来自热砂子分离系统中第一级旋风燃烧分离器的高温砂子、旋风反应分离器第一组第二单元的高温气体一起进入旋风反应分离器第一组第一单元中；生物质原料在受热以及气化介质作用下气化生成固体焦炭、不可冷凝气体、水蒸气与焦油，其中固体焦炭和热砂子在生物质热解气化系统的多级旋风反应分离器中，自上而下运动并在气化介质作用下发生气化反应，最后获得的固体焦炭、灰分和砂子的混合物进入流化床焦炭燃烧系统中；The biomass raw material is sent to the first unit of the cyclone reaction separator of the biomass pyrolysis gasification system through the hopper and the feeding system; at the same time, the high-temperature sand from the first stage cyclone combustion separator in the hot sand separation system, The high-temperature gas from the first group and the second unit of the cyclone reaction separator enters the first group and the first unit of the cyclone reaction separator; the biomass raw material is gasified under the action of heat and gasification medium to generate solid coke, non-condensable gas, and water vapor With tar, solid coke and hot sand move from top to bottom in the multi-stage cyclone reaction separator of the biomass pyrolysis gasification system and undergo gasification reaction under the action of gasification medium, and finally the solid coke and ash obtained The mixture with sand enters the fluidized bed coke combustion system;
生物质热解气化系统中旋风反应分离器第一组第一单元排气口排出的不可冷凝气体、水蒸气和焦油的混合气进入焦油催化裂解系统中旋风反应分离器第二组第一单元，同时，来自旋风反应分离器第二组第二单元的催化剂也一起进入旋风反应分离器第二组第一单元；混合气在焦油催化裂解系统的多级旋风反应分离器中自下而上运行，其中的焦油在自上而下的催化剂作用下发生催化裂解反应，最后获得不可冷凝气体和水蒸气的混合气，其中部分作为气化介质送入生物质热解气化系统中旋风反应分离器第一组最末单元循环使用，另外部分则经冷却后获得极低焦油含量的富氢合成气；The mixture of non-condensable gas, water vapor and tar discharged from the exhaust port of the first unit of the cyclone reaction separator in the biomass pyrolysis gasification system enters the first unit of the second group of the cyclone reaction separator in the tar catalytic cracking system At the same time, the catalyst from the second unit of the cyclone reaction separator also enters the first unit of the second group of the cyclone reaction separator; the mixed gas runs from bottom to top in the multi-stage cyclone reaction separator of the tar catalytic cracking system , the tar in it undergoes a catalytic cracking reaction under the action of a top-down catalyst, and finally obtains a mixture of non-condensable gas and water vapor, part of which is sent as a gasification medium to the cyclone reaction separator in the biomass pyrolysis gasification system The last unit of the first group is recycled, and the other part is cooled to obtain hydrogen-rich synthesis gas with extremely low tar content;
生物质热解气化系统中旋风反应分离器第一组最末单元获得的固体焦炭、砂子和灰分的混合物送入流化床焦炭燃烧系统，并供入过量空气燃烧焦炭加热砂子；The mixture of solid coke, sand and ash obtained from the first unit of the cyclone reaction separator in the biomass pyrolysis gasification system is sent to the fluidized bed coke combustion system, and excess air is supplied to burn the coke to heat the sand;
流化床焦炭燃烧系统的燃烧产物进入热砂子分离系统中，第一级旋风分离器分离获得的热砂子送入生物质热解气化系统的旋风反应分离器第一组第一单元中，作为热载体提供生物质热解所需的热量；The combustion products of the fluidized bed coke combustion system enter the hot sand separation system, and the hot sand separated by the first-stage cyclone separator is sent to the first unit of the cyclone reaction separator of the biomass pyrolysis gasification system, as The heat carrier provides the heat required for biomass pyrolysis;
热砂子分离系统中第二级旋风分离器出口获得的富氧烟气通入流化床催化剂再生系统中，积碳失活的催化剂与富氧烟气中的高温O2反应，实现催化剂的再生；The oxygen-enriched flue gas obtained from the outlet of the second-stage cyclone separator in the hot sand separation system is passed into the fluidized bed catalyst regeneration system, and the carbon-deactivated catalyst reacts with the high-temperature O2 in the oxygen-enriched flue gas to realize the regeneration of the catalyst ;
流化床催化剂再生系统的产物进入催化剂分离系统中，单级旋风分离器分离获得的再生催化剂送入焦油催化裂解系统中旋风反应分离器第二组最末单元，用于焦油的催化裂解。The product of the fluidized bed catalyst regeneration system enters the catalyst separation system, and the regenerated catalyst separated by the single-stage cyclone separator is sent to the second final unit of the cyclone reaction separator in the tar catalytic cracking system for catalytic cracking of tar.
所述催化剂为天然矿石、炭或镍基催化剂。The catalyst is natural ore, carbon or nickel-based catalyst.
所述天然矿石为白云石、石灰石或橄榄石。The natural ore is dolomite, limestone or olivine.
所述流化床焦炭燃烧系统的过量空气系数为1.2-2.0。The excess air ratio of the fluidized bed coke combustion system is 1.2-2.0.
所述流化床焦炭燃烧系统的反应温度为800-1000℃。The reaction temperature of the fluidized bed coke combustion system is 800-1000°C.
本发明的有益效果为：The beneficial effects of the present invention are:
本发明所述的生物质热解气化工艺，是以生物质气化获得的气体产物（包括H2O、CO2、CO、H2、CH4等成分）为气化介质，使生物质在受热作用下发生分解并与H2O、CO2等发生反应，从而获得富氢合成气。该工艺的实施主要有两大技术难题：（1）生物质在H2O、CO2等气氛下的气化反应，速度较慢，难以充分反应；（2）气化过程会产生较多的焦油。针对这两个问题，本发明提出了基于多级旋风反应/分离器的生物质热解气化系统和焦油催化裂解系统，分别对生物质气化和焦油催化裂解进行充分的反应；并通过焦炭在过量空气下的燃烧加热砂子提供生物质热解所需的热量，并获得富氧烟气对失活催化剂进行再生；生物质气化介质中不含N2但含有较多的H2O和CO2（可实现生物质的水蒸气气化和CO2气化），确保气化气体不含N2且H2含量较高，从而获得富氢合成气。The biomass pyrolysis gasification process described in the present invention uses gas products obtained from biomass gasification (including H 2 O, CO 2 , CO, H 2 , CH 4 , etc.) Under the action of heat, it decomposes and reacts with H 2 O, CO 2, etc. to obtain hydrogen-rich synthesis gas. There are two main technical problems in the implementation of this process: (1) The gasification reaction of biomass in H 2 O, CO 2 and other atmospheres is slow and difficult to fully react; (2) The gasification process will produce more tar. In view of these two problems, the present invention proposes a biomass pyrolysis gasification system and a tar catalytic cracking system based on a multi-stage cyclone reaction/separator, which fully react to biomass gasification and tar catalytic cracking respectively; Combustion heating sand under excess air provides the heat required for biomass pyrolysis, and obtains oxygen-rich flue gas to regenerate the deactivated catalyst; the biomass gasification medium does not contain N 2 but contains more H 2 O and CO 2 (which can realize steam gasification of biomass and CO 2 gasification), ensure that the gasification gas does not contain N 2 and has a high H 2 content, so as to obtain hydrogen-rich synthesis gas.
附图说明 Description of drawings
图1为本发明所述的生物质快速热解气化装置结构示意图；Fig. 1 is the structural schematic diagram of biomass quick pyrolysis gasification device described in the present invention;
图中标号：Labels in the figure:
1-料斗；2-进料系统；3-生物质热解气化系统；4-焦油催化裂解系统；5-流化床焦炭燃烧系统；6-热砂子分离系统；7-流化床催化剂再生系统；8-催化剂分离系统。1-hopper; 2-feeding system; 3-biomass pyrolysis gasification system; 4-tar catalytic cracking system; 5-fluidized bed coke combustion system; 6-hot sand separation system; 7-fluidized bed catalyst regeneration system; 8-catalyst separation system.
具体实施方式 Detailed ways
本发明提供了一种生物质热解气化与焦油催化裂解的装置与方法，下面结合具体实施方式对本发明做进一步说明。The present invention provides a device and method for pyrolysis gasification of biomass and catalytic cracking of tar. The present invention will be further described below in combination with specific embodiments.
各实施例中的装置结构相同，如图1所示。The device structure in each embodiment is the same, as shown in FIG. 1 .
料斗1的出口与进料系统2的入口相连，进料系统2为螺旋进料器；流化床焦炭燃烧系统5的底部与鼓风机相连，直接供入过量空气，其侧壁下端还有一个入口用于补充新砂子；热砂子分离系统6包括两级旋风分离器，其中第一级旋风分离器a的进口与流化床焦炭燃烧系统5的出口相连，排气口与第二级旋风分离器b的进口相连，第二级旋风分离器b的出气口与流化床催化剂再生系统7的底部气体入口相连，排料口与集灰箱相连，直接收集飞灰；流化床催化剂再生系统7的侧壁下端设有一个入口用于补充新催化剂；催化剂分离系统8为单级旋风分离器，其进口与流化床催化剂再生系统7的出口相连。The outlet of the hopper 1 is connected to the inlet of the feeding system 2, which is a screw feeder; the bottom of the fluidized bed
生物质热解气化系统3包括多个旋风反应分离器；所述的多个旋风反应分离器自上而下串联，定义最上面的旋风反应分离器为旋风反应分离器第一组第一单元I，向下依次为旋风反应分离器第一组第二单元II，······，旋风反应分离器第一组最末单元N，其中，N为不小于2的整数；焦油催化裂解系统4包括多个旋风反应分离器；所述的多个旋风反应分离器自下而上串联，定义最下面的旋风反应分离器为旋风反应分离器第二组第一单元i，向上依次为旋风反应分离器第二组第二单元ii，······，旋风反应分离器第二组最末单元n，其中，n为不小于2的整数。The biomass
旋风反应分离器第一组第一单元I的排料口与旋风反应分离器第一组第二单元II的进料口相连，旋风反应分离器第一组第二单元II的排气口与旋风反应分离器第一组第一单元I的进气口相连；旋风反应分离器第一组第二单元II的排料口与旋风反应分离器第一组第三单元III的进料口相连，旋风反应分离器第一组第三单元III的排气口与旋风反应分离器第一组第二单元II的进气口相连，依次类推至旋风反应分离器第一组最末单元N；其中，旋风反应分离器第一组第一单元I的侧部还有两个进料口，其中一个进料口与进料系统2的出口相连，另一个进料口与热砂子分离系统6中第一级旋风分离器a的排料口相连，旋风反应分离器第一组第一单元I的排气口与焦油催化裂解系统4中旋风反应分离器第二组第一单元i的进气口相连；旋风反应分离器第一组最末单元N的排料口和进气口分别与流化床焦炭燃烧系统5的侧壁下端开口、旋风反应分离器第二组最末单位n的出气口相连。The discharge port of the first unit I of the first group of the cyclone reaction separator is connected with the feed port of the second unit II of the first group of the cyclone reaction separator, and the exhaust port of the second unit II of the first group of the cyclone reaction separator is connected with the cyclone reaction separator. The air inlet of the first unit I of the first group of the reaction separator is connected; the discharge port of the second unit II of the first group of the cyclone reaction separator is connected with the feed port of the third unit III of the first group of the cyclone reaction separator. The exhaust port of the third unit III of the first group of reaction separator is connected with the air inlet of the second unit II of the first group of cyclone reaction separator, and so on to the last unit N of the first group of cyclone reaction separator; wherein, the cyclone There are also two feed inlets on the side of the first unit I of the reaction separator, one of which is connected to the outlet of the feed system 2, and the other feed inlet is connected to the first stage in the hot
旋风反应分离器第二组第一单元i的排气口与旋风反应分离器第二组第二单元ii的进气口相连，旋风反应分离器第二组第二单元ii的排料口与旋风反应分离器第二组第一单元i的进料口相连；旋风反应分离器第二组第二单元ii的排气口与旋风反应分离器第二组第三单元iii的进气口相连，旋风反应分离器第二组第三单元iii的排料口与旋风反应分离器第二组第二单元ii的进料口相连，依次类推至旋风反应分离器第二组最末单元n；其中，旋风反应分离器第二组第一单元i的进气口和排料口分别与生物质热解气化系统3中旋风反应分离器第一组第一单元I的排气口和流化床催化剂再生系统7的侧壁下端开口相连；旋风反应分离器第二组最末单元n的进料口与催化剂分离系统8的排料口相连，旋风反应分离器第二组最末单元n的排气口分为两路，一路与生物质热解气化系统3中旋风反应分离器第一组最末单元N的进气口相连，另一路直接收集极低焦油含量的富氢合成气。The exhaust port of the second group of the first unit i of the cyclone reaction separator is connected with the inlet port of the second group of the second unit ii of the cyclone reaction separator, and the discharge port of the second group of the second unit ii of the cyclone reaction separator is connected with the cyclone The feed port of the first unit i of the second group of the reaction separator is connected; the exhaust port of the second unit ii of the second group of the cyclone reaction separator is connected with the inlet of the third unit iii of the second group of the cyclone reaction separator, and the cyclone The discharge port of the second group of the third unit iii of the reaction separator is connected with the feed port of the second group of the second unit ii of the cyclone reaction separator, and so on to the last unit n of the second group of the cyclone reaction separator; wherein, the cyclone The inlet port and discharge port of the first unit i of the second group of reaction separator are respectively regenerated with the exhaust port of the first unit I of the first group I of the cyclone reaction separator in the biomass
下述实施例中的百分含量，如无特殊说明均为质量百分含量，s表示秒。The percentages in the following examples are mass percentages unless otherwise specified, and s represents seconds.
实施例1Example 1
采用上述装置以玉米秆为原料、白云石为催化剂、砂子为热载体进行热解气化与焦油催化裂解实验。将玉米秆送入含有3个旋风反应分离器的生物质热解气化系统，进料量为100kg/h，玉米秆经气化反应后获得760℃的固体产物（砂子、焦炭和灰分的混合物）；生物质热解气化系统生成的混合气（焦油、水蒸气和不可冷凝气的混合气）进入含有3个旋风反应分离器的焦油催化裂解系统，混合气经催化裂解反应后获得温度为840℃的水蒸气和不可冷凝气的混合气，经冷凝后获得富氢合成气，同时排出温度为720℃的失活催化剂送入流化床催化剂再生系统中。The experiment of pyrolysis gasification and tar catalytic cracking was carried out by using the above device with corn stalk as raw material, dolomite as catalyst and sand as heat carrier. The corn stalks are sent to the biomass pyrolysis gasification system containing 3 cyclone reaction separators, the feed rate is 100kg/h, and the solid products (a mixture of sand, coke and ash) at 760°C are obtained after the corn stalks are gasified ); the mixed gas (mixed gas of tar, water vapor and non-condensable gas) generated by the biomass pyrolysis gasification system enters the tar catalytic cracking system containing 3 cyclone reaction separators, and the mixed gas obtains a temperature of The mixture of water vapor and non-condensable gas at 840°C is condensed to obtain hydrogen-rich synthesis gas, and the deactivated catalyst with a temperature of 720°C is discharged and sent to the fluidized bed catalyst regeneration system.
从生物质热解气化系统获得的760℃的固体产物（砂子、焦炭和灰分的混合物），送入一内径为700mm、高度为3m的流化床焦炭燃烧系统内进行燃烧，过量空气系数为1.3，反应温度为920℃，反应获得的热砂子送入生物质热解气化系统中用于气化过程的供热，同时获得920℃的富氧烟气送入流化床催化剂再生系统内；从焦油催化裂解系统中排出的720℃的失活催化剂，经流化床催化剂再生系统和催化剂分离系统后，得到880℃的活性催化剂送入焦油催化裂解系统中用于焦油的催化裂解。The 760°C solid product (a mixture of sand, coke and ash) obtained from the biomass pyrolysis gasification system is sent to a fluidized bed coke combustion system with an inner diameter of 700mm and a height of 3m for combustion. The excess air coefficient is 1.3, the reaction temperature is 920°C, the hot sand obtained from the reaction is sent to the biomass pyrolysis gasification system for heat supply in the gasification process, and the oxygen-enriched flue gas obtained at 920°C is sent to the fluidized bed catalyst regeneration system ; The 720°C deactivated catalyst discharged from the tar catalytic cracking system, after passing through the fluidized bed catalyst regeneration system and the catalyst separation system, the 880°C active catalyst is sent to the tar catalytic cracking system for catalytic cracking of tar.
实施例2Example 2
采用与实施例1结构相同的装置，以玉米秆为原料、NiO/Al2O3为催化剂、砂子为热载体原料进行热解气化与焦油催化裂解实验。玉米秆进料量为100kg/h，经热解气化系统反应后获得750℃的固体产物（砂子、焦炭和灰分的混合物），气化获得的混合气（焦油、水蒸气和不可冷凝气的混合气）经催化裂解反应后获得温度为800℃的水蒸气和不可冷凝气的混合气，经冷凝后获得富氢合成气，同时排出温度为700℃的失活催化剂送入流化床催化剂再生系统中。Using the device with the same structure as in Example 1, corn stalks were used as raw material, NiO/Al 2 O 3 was used as catalyst, and sand was used as heat carrier material to conduct pyrolysis gasification and tar catalytic cracking experiments. The feed rate of corn stalks is 100kg/h, and the solid product (a mixture of sand, coke and ash) at 750 ° C is obtained after the reaction of the pyrolysis gasification system, and the mixed gas (tar, water vapor and non-condensable gas) obtained by gasification Mixed gas) After the catalytic cracking reaction, the mixed gas of water vapor and non-condensable gas with a temperature of 800 ° C is obtained, and hydrogen-rich synthesis gas is obtained after condensation. At the same time, the deactivated catalyst with a temperature of 700 ° C is discharged and sent to the fluidized bed for catalyst regeneration. system.
固体产物（砂子、焦炭和灰分的混合物）在流化床焦炭燃烧系统内进行燃烧，过量空气系数为1.4，反应温度为900℃，反应获得的热砂子送入生物质热解气化系统中用于气化过程的供热，同时获得900℃的富氧烟气送入流化床催化剂再生系统内；700℃的失活催化剂经流化床催化剂再生系统和催化剂分离系统后，得到850℃的活性催化剂送入焦油催化裂解系统中用于焦油的催化裂解。The solid product (a mixture of sand, coke and ash) is burned in a fluidized bed coke combustion system with an excess air ratio of 1.4 and a reaction temperature of 900°C. The hot sand obtained from the reaction is sent to the biomass pyrolysis gasification system for use In the heat supply of the gasification process, the oxygen-enriched flue gas obtained at 900°C is fed into the fluidized bed catalyst regeneration system; the deactivated catalyst at 700°C passes through the fluidized bed catalyst regeneration system and catalyst separation system to obtain 850°C flue gas The active catalyst is sent to the tar catalytic cracking system for catalytic cracking of tar.
实施例3Example 3
与实施例1采用的装置相比，生物质热解气化系统的旋风反应分离器的个数改为4个，其余结构相同；以稻壳为原料、NiO/SiO2为催化剂、砂子为热载体进行热解气化与焦油催化裂解实验。稻壳进料量为100kg/h，经热解气化系统反应后获得700℃的固体产物（砂子、焦炭和灰分的混合物），气化获得的混合气（焦油、水蒸气和不可冷凝气的混合气）经催化裂解反应后获得温度为770℃的水蒸气和不可冷凝气的混合气，经冷凝后获得富氢合成气，同时排出温度为680℃的失活催化剂送入流化床催化剂再生系统中。Compared with the device used in Example 1, the number of cyclone reaction separators in the biomass pyrolysis gasification system is changed to 4, and the rest of the structure is the same; with rice husk as raw material, NiO/ SiO as catalyst, sand as heat The carrier was subjected to pyrolysis gasification and tar catalytic cracking experiments. The feed rate of rice husk is 100kg/h, and the solid product (a mixture of sand, coke and ash) at 700°C is obtained after the reaction of the pyrolysis gasification system, and the mixed gas (tar, water vapor and non-condensable gas) obtained by gasification Mixed gas) After the catalytic cracking reaction, the mixed gas of water vapor and non-condensable gas with a temperature of 770 ° C is obtained, and hydrogen-rich synthesis gas is obtained after condensation. At the same time, the deactivated catalyst with a temperature of 680 ° C is sent to the fluidized bed catalyst for regeneration system.
固体产物（砂子、焦炭和灰分的混合物）在流化床焦炭燃烧系统内进行燃烧，过量空气系数为1.5，反应温度为880℃，反应获得的热砂子送入生物质热解气化系统中用于气化过程的供热，同时获得880℃的富氧烟气送入流化床催化剂再生系统内；680℃的失活催化剂经流化床催化剂再生系统和催化剂分离系统后，得到810℃的活性催化剂送入焦油催化裂解系统中用于焦油的催化裂解。The solid product (a mixture of sand, coke and ash) is burned in a fluidized bed coke combustion system with an excess air ratio of 1.5 and a reaction temperature of 880°C. The hot sand obtained from the reaction is sent to the biomass pyrolysis gasification system for use In the heat supply of the gasification process, the oxygen-enriched flue gas obtained at 880°C is sent to the fluidized bed catalyst regeneration system; the deactivated catalyst at 680°C is passed through the fluidized bed catalyst regeneration system and the catalyst separation system to obtain The active catalyst is sent to the tar catalytic cracking system for catalytic cracking of tar.
实施例4Example 4
与实施例1采用的装置相比，焦油催化裂解系统的旋风反应分离器的个数改为4个，其余结构相同；以锯末为原料、橄榄石为催化剂、砂子为热载体进行热解气化与焦油催化裂解实验。锯末进料量为100kg/h，经热解气化系统反应后获得730℃的固体产物（砂子、焦炭和灰分的混合物），气化获得的混合气（焦油、水蒸气和不可冷凝气的混合气）经催化裂解反应后获得温度为760℃的水蒸气和不可冷凝气的混合气，经冷凝后获得富氢合成气，同时排出温度为660℃的失活催化剂送入流化床催化剂再生系统中。Compared with the device used in Example 1, the number of cyclone reaction separators in the tar catalytic cracking system is changed to 4, and the rest of the structure is the same; sawdust is used as raw material, olivine is used as catalyst, and sand is used as heat carrier for pyrolysis and gasification Experiments with catalytic cracking of tar. The feed rate of sawdust is 100kg/h, and the solid product (a mixture of sand, coke and ash) at 730°C is obtained after the reaction of the pyrolysis gasification system, and the mixed gas obtained by gasification (the mixture of tar, water vapor and non-condensable gas Gas) After the catalytic cracking reaction, the mixed gas of water vapor and non-condensable gas with a temperature of 760 ° C is obtained, and hydrogen-rich synthesis gas is obtained after condensation, and the deactivated catalyst with a temperature of 660 ° C is discharged and sent to the fluidized bed catalyst regeneration system middle.
固体产物（砂子、焦炭和灰分的混合物）在流化床焦炭燃烧系统内进行燃烧，过量空气系数为1.4，反应温度为910℃，反应获得的热砂子送入生物质热解气化系统中用于气化过程的供热，同时获得910℃的富氧烟气送入流化床催化剂再生系统内；660℃的失活催化剂经流化床催化剂再生系统和催化剂分离系统后，得到820℃的活性催化剂送入焦油催化裂解系统中用于焦油的催化裂解。The solid product (a mixture of sand, coke and ash) is burned in a fluidized bed coke combustion system with an excess air ratio of 1.4 and a reaction temperature of 910°C. The hot sand obtained from the reaction is sent to the biomass pyrolysis gasification system for use In the heat supply of the gasification process, the oxygen-enriched flue gas obtained at 910°C is fed into the fluidized bed catalyst regeneration system; the deactivated catalyst at 660°C is passed through the fluidized bed catalyst regeneration system and the catalyst separation system to obtain The active catalyst is sent to the tar catalytic cracking system for catalytic cracking of tar.
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