技术领域technical field
本发明涉及生物质化学链气化方法及装置，尤其涉及一种基于氧载体/碳载体的生物质化学链气化方法及装置。The invention relates to a biomass chemical chain gasification method and device, in particular to a biomass chemical chain gasification method and device based on an oxygen carrier/carbon carrier.
背景技术Background technique
通过气化制取以CO与H2为主的合成气是生物质能源利用的一个重要方向。传统的生物质气化技术是通过纯氧、水蒸汽作为气化剂，在1000～1200℃高温条件下使生物质中的可燃成分转化为可燃气。化学链技术为生物质气化提供了一条技术思路。化学链气化是化学链燃烧(CLC)的一种扩展应用，通过利用氧载体中的晶格氧使生物质燃料部分氧化成可燃气，反应后的氧载体可通过在空气中煅烧使晶格氧再生。因此，化学链气化技术可节省纯氧制备的成本。为提高固体燃料气化产物中H2的含量，近年来兴起了一种基于气体吸收体气化法的强化制氢工艺，该工艺在固体燃料水蒸汽气化过程中引入CO2吸收剂(CaO)，通过捕获和移出化学平衡中的CO2，提高H2的产量。同时，该技术通过CaO碳酸化-煅烧的循环过程，实现CO2的捕获，并实现CaO吸收剂的再生。Production of syngas mainly composed of CO and H2 through gasification is an important direction of biomass energy utilization. The traditional biomass gasification technology uses pure oxygen and water vapor as the gasification agent to convert combustible components in biomass into combustible gas under high temperature conditions of 1000-1200 °C. Chemical chain technology provides a technical idea for biomass gasification. Chemical looping gasification is an extended application of chemical looping combustion (CLC). By using the lattice oxygen in the oxygen carrier to partially oxidize the biomass fuel into combustible gas, the reacted oxygen carrier can be calcined in the air to make the lattice Oxygen regeneration. Therefore, the chemical looping gasification technology can save the cost of pure oxygen production. In order to increase theH2 content in solid fuel gasification products, an enhanced hydrogen production process based on the gas absorber gasification method has emerged in recent years. This process introducesCO2 absorbent (CaO ), to increase the production of H2 by capturing and removing CO2 from chemical equilibrium. At the same time, the technology realizes the capture ofCO2 and the regeneration of CaO absorbent through the cyclic process of CaO carbonation-calcination.
在化学链气化中，由于氧载体的氧化作用使得合成气中CO2含量较高，导致热值较低。通过引入CaO作为碳载体可有效降低CO2含量并提高H2的产量，有利于提高合成气的质量。同时氧载体的氧化作用也可提高CaO吸收体法中固体燃料的转化率。In chemical looping gasification, theCO2 content in the syngas is higher due to the oxidation of oxygen carriers, resulting in a lower calorific value. The introduction of CaO as a carbon carrier can effectively reduceCO2 content and increaseH2 production, which is beneficial to improve the quality of syngas. At the same time, the oxidation of oxygen carrier can also improve the conversion rate of solid fuel in CaO absorber method.
发明内容Contents of the invention
本发明目的在于结合化学链气化与CaO吸收体法各自优势，优化现有的化学链气化工艺，提供一种基于氧载体/碳载体的生物质化学链气化方法及装置，以提高生物质的能源利用效率并有效分离反应生成的CO2。The purpose of the present invention is to combine the respective advantages of chemical looping gasification and CaO absorber method, optimize the existing chemical looping gasification process, and provide a biomass chemical looping gasification method and device based on oxygen carrier/carbon carrier, so as to improve biological The energy utilization efficiency of the material and the effective separation of CO2 generated by the reaction.
本发明通过下述技术方案实现：The present invention realizes through following technical scheme:
一种基于氧载体/碳载体的生物质化学链气化装置，包括空气反应器1、第二隔离器5-2、煅烧反应器3、第一隔离器5-1、气化反应器2、第三旋风分离器4-3、第二旋风分离器4-2、第一旋风分离器4-1；A biomass chemical chain gasification device based on oxygen carrier/carbon carrier, comprising an air reactor 1, a second isolator 5-2, a calcining reactor 3, a first isolator 5-1, a gasification reactor 2, The third cyclone separator 4-3, the second cyclone separator 4-2, the first cyclone separator 4-1;
所述空气反应器1、第二隔离器5-2、煅烧反应器3、第一隔离器5-1、气化反应器2通过管路按照顺序依次连通；The air reactor 1, the second isolator 5-2, the calcining reactor 3, the first isolator 5-1, and the gasification reactor 2 are connected in sequence through pipelines;
所述煅烧反应器3顶部与第三旋风分离器4-3的进气口连通，第三旋风分离器4-3底部的固体颗粒排放口连通煅烧反应器3；第三旋风分离器4-3的排气管路通过一阀门连通煅烧反应器3底部的进气口；The top of the calcining reactor 3 communicates with the air inlet of the third cyclone separator 4-3, and the solid particle discharge port at the bottom of the third cyclone separator 4-3 communicates with the calcining reactor 3; the third cyclone separator 4-3 The exhaust pipeline is connected to the air inlet at the bottom of the calcining reactor 3 through a valve;
所述气化反应器2的排气口与第一旋风分离器4-1的进气口连通；第一旋风分离器4-1的固体颗粒排放口通过管路伸入气化反应器2内底部；气化反应器2排气口与第二旋风分离器4-2进气口连通；The exhaust port of the gasification reactor 2 communicates with the air inlet of the first cyclone separator 4-1; the solid particle discharge port of the first cyclone separator 4-1 extends into the gasification reactor 2 through a pipeline Bottom; the gasification reactor 2 exhaust port communicates with the second cyclone separator 4-2 air intake;
所述第二隔离器5-2、煅烧反应器3和气化反应器2的底部，分别通过一带阀门的管路通入H2O；The bottoms of the second isolator 5-2, the calcining reactor 3 and the gasification reactor 2 are respectively fed withH2O through a pipeline with a valve;
所述空气反应器1的底部通入空气。Air is fed into the bottom of the air reactor 1 .
所述煅烧反应器3的底侧设有第二螺旋进料器6-2；气化反应器2的底侧设有第一螺旋进料器6-1。The bottom side of the calcining reactor 3 is provided with a second screw feeder 6-2; the bottom side of the gasification reactor 2 is provided with a first screw feeder 6-1.
所述气化反应器2与煅烧反应器3为鼓泡流化床；空气反应器1为快速流化床。The gasification reactor 2 and the calcining reactor 3 are bubbling fluidized beds; the air reactor 1 is a fast fluidized bed.
所述气化反应器2、煅烧反应器3、空气反应器1以及第二隔离器5-2和第一隔离器5-1的内底部分别设置有多孔布风板。The gasification reactor 2, the calcination reactor 3, the air reactor 1, and the inner bottoms of the second isolator 5-2 and the first isolator 5-1 are respectively provided with porous air distribution plates.
一种基于氧载体/碳载体的生物质化学链气化的方法，可通过如下步骤实现：A method for chemical chain gasification of biomass based on oxygen carrier/carbon carrier can be realized through the following steps:
步骤一：将氧载体与碳载体颗粒预先送入气化反应器2中作为床料，将床料预热至目标反应温度；Step 1: pre-feeding the oxygen carrier and carbon carrier particles into the gasification reactor 2 as bed material, and preheating the bed material to the target reaction temperature;
步骤二：生物质燃料由第一螺旋进料器6-1送入气化反应器2，在650～750℃条件下与氧载体、碳载体与水蒸汽反应，在碳载体的吸收作用下，反应生成的CO2被吸收，并由于化学平衡作用在气化反应器2中生成高H2/CO比的合成气；所述合成气中H2与CO的体积比是5.0～6.9；Step 2: The biomass fuel is fed into the gasification reactor 2 by the first screw feeder 6-1, and reacts with the oxygen carrier, carbon carrier and water vapor under the condition of 650-750°C, and under the absorption of the carbon carrier, The CO2 generated by the reaction is absorbed, and due to the chemical balance, a synthesis gas with a high H2 /CO ratio is generated in the gasification reactor 2; the volume ratio of H2 to CO in the synthesis gas is 5.0-6.9;
步骤三：气化反应器2生成的合成气经过第二旋风分离器4-2的分离，将生物质通过第二旋风分离器4-2底部的固体颗粒(灰)排放口排出，在第二旋风分离器4-2顶部的排气口得到步骤二所述合成气；反应后的固体颗粒(包括氧载体、碳载体以及残余生物质半焦)经第一隔离器5-1输送至煅烧反应器3；Step 3: the synthesis gas generated by the gasification reactor 2 is separated through the second cyclone separator 4-2, and the biomass is discharged through the solid particle (ash) discharge port at the bottom of the second cyclone separator 4-2, The exhaust port at the top of the cyclone separator 4-2 obtains the synthesis gas described in step 2; the reacted solid particles (including oxygen carrier, carbon carrier and residual biomass semi-coke) are transported to the calcination reaction through the first separator 5-1 device 3;
步骤四：在煅烧反应器3中，煅烧温度设置在900～950℃，并从煅烧反应器3底部进气口通入CO2/H2O作为流化气，将气化反应后的碳载体分解，使其中的活性组分CaO得以再生；同时煅烧生成的气体进入第三旋风分离器4-3进行气固分离，使第三旋风分离器4-3的排气口得到H2O/CO2混合气；(纯CO2应在H2O/CO2混合气冷凝后得到)Step 4: In the calcination reactor 3, the calcination temperature is set at 900-950°C, and CO2 /H2 O is introduced from the gas inlet at the bottom of the calcination reactor 3 as fluidization gas, and the carbon carrier after the gasification reaction is Decompose, so that the active component CaO can be regenerated; at the same time, the gas generated by calcination enters the third cyclone separator 4-3 for gas-solid separation, so that the exhaust port of the third cyclone separator 4-3 can obtain H2 O/CO2 mixed gas; (pure CO2 should be obtained after condensation of H2 O/CO2 mixed gas)
将得到的CO2/H2O混合气一部分进行后续冷凝与封存，另一部分引至煅烧反应器3的底部进气口作为流化气；Part of the obtained CO2 /H2 O mixed gas is subjected to subsequent condensation and storage, and the other part is introduced to the bottom air inlet of the calcining reactor 3 as fluidizing gas;
步骤五：经煅烧的固体颗粒经第二隔离器5-2进入空气反应器1的底部，设置空气反应器1的温度为900～950℃，被还原的氧载体与空气反应使氧载体中的晶格氧得到恢复，并由空气带出空气反应器1送至第一旋风分离器4-1；经第一旋风分离器4-1的分离，贫氧空气从第一旋风分离器4-1顶部排气口排出，氧载体/碳载体颗粒从第一旋风分离器4-1底部返回到气化反应器2内，再次与生物质燃料反应。Step 5: The calcined solid particles enter the bottom of the air reactor 1 through the second isolator 5-2, and the temperature of the air reactor 1 is set at 900-950°C, and the reduced oxygen carrier reacts with the air to make the oxygen carrier The lattice oxygen is recovered, and is taken out of the air reactor 1 by the air and sent to the first cyclone separator 4-1; after being separated by the first cyclone separator 4-1, the oxygen-depleted air is discharged from the first cyclone separator 4-1 The top exhaust port is discharged, and the oxygen carrier/carbon carrier particles return to the gasification reactor 2 from the bottom of the first cyclone separator 4-1, and react with the biomass fuel again.
上述步骤五所述氧载体颗粒为铁矿石，其活性组分为Fe2O3；碳载体颗粒为生石灰，其活性组分为CaO，在煅烧反应器3中煅烧石灰石获得。The oxygen carrier particle mentioned in step five is iron ore, whose active component is Fe2 O3 ; the carbon carrier particle is quicklime, whose active component is CaO, which is obtained by calcining limestone in the calcining reactor 3 .
上述步骤五所述气化反应器2内的氧载体可由第一螺旋进料器6-1补给；The oxygen carrier in the gasification reactor 2 described in the above step five can be replenished by the first screw feeder 6-1;
上述步骤四所述煅烧反应器3中的碳载体可由第二螺旋进料器6-2送入石灰石补给。The carbon carrier in the calcining reactor 3 described in the above step 4 can be replenished with limestone through the second screw feeder 6-2.
本发明相对于现有技术，具有如下的优点及效果：Compared with the prior art, the present invention has the following advantages and effects:
(1)通过化学链的方式对生物质燃料进行部分氧化，氧载体可循环使用，节省了传统气化方式中纯氧制备的成本；(1) The biomass fuel is partially oxidized by means of a chemical chain, and the oxygen carrier can be recycled, which saves the cost of pure oxygen preparation in the traditional gasification method;
(2)采用CaO吸收体法捕获气化中生成的CO2，可提高合成气中H2的浓度，克服了直接化学链气化中CO2含量较高的问题；CaO的碳酸化-煅烧循环可有效分离气化反应中生成的CO2与H2，节省了后续分离提纯合成气的成本；(2) Using the CaO absorber method to capture the CO2 generated in the gasification can increase the concentration of H2 in the syngas and overcome the problem of high CO2 content in the direct chemical looping gasification; the carbonation-calcination cycle of CaO It can effectively separate CO2 and H2 generated in the gasification reaction, saving the cost of subsequent separation and purification of syngas;
(3)氧载体与碳载体有助于焦油催化分解，提高合成气产量，提高反应系统的稳定性；(3) Oxygen carrier and carbon carrier contribute to the catalytic decomposition of tar, increase the production of synthesis gas, and improve the stability of the reaction system;
(4)CaO的存在可抑制灰分中碱金属引起的氧载体烧结问题，提高循环反应的稳定性；(4) The presence of CaO can inhibit the sintering of oxygen carriers caused by alkali metals in the ash, and improve the stability of the cycle reaction;
(5)采用廉价且环境友好的铁矿石/石灰石颗粒作为氧载体/碳载体，运行成本低，且清洁环保。(5) Using cheap and environmentally friendly iron ore/limestone particles as the oxygen carrier/carbon carrier, the operating cost is low, and it is clean and environmentally friendly.
附图说明Description of drawings
图1为本发明基于氧载体/碳载体的生物质化学链气化装置示意图。Fig. 1 is a schematic diagram of a biomass chemical looping gasification device based on an oxygen carrier/carbon carrier according to the present invention.
具体实施方式Detailed ways
下面结合具体实施例对本发明作进一步具体详细描述。The present invention will be described in further detail below in conjunction with specific embodiments.
实施例Example
如图1所示。本发明公开了一种基于氧载体/碳载体的生物质化学链气化装置，包括空气反应器1、第二隔离器5-2、煅烧反应器3、第一隔离器5-1、气化反应器2、第三旋风分离器4-3、第二旋风分离器4-2、第一旋风分离器4-1；As shown in Figure 1. The invention discloses a biomass chemical chain gasification device based on oxygen carrier/carbon carrier, which comprises an air reactor 1, a second isolator 5-2, a calcining reactor 3, a first isolator 5-1, a gasification Reactor 2, third cyclone separator 4-3, second cyclone separator 4-2, first cyclone separator 4-1;
所述空气反应器1、第二隔离器5-2、煅烧反应器3、第一隔离器5-1、气化反应器2通过管路按照顺序依次连通；The air reactor 1, the second isolator 5-2, the calcining reactor 3, the first isolator 5-1, and the gasification reactor 2 are connected in sequence through pipelines;
所述煅烧反应器3顶部与第三旋风分离器4-3的进气口连通，第三旋风分离器4-3底部的固体颗粒排放口连通煅烧反应器3；第三旋风分离器4-3的排气管路通过一阀门连通煅烧反应器3底部的进气口；The top of the calcining reactor 3 communicates with the air inlet of the third cyclone separator 4-3, and the solid particle discharge port at the bottom of the third cyclone separator 4-3 communicates with the calcining reactor 3; the third cyclone separator 4-3 The exhaust pipeline is connected to the air inlet at the bottom of the calcining reactor 3 through a valve;
所述气化反应器2的排气口与第一旋风分离器4-1的进气口连通；第一旋风分离器4-1的固体颗粒排放口通过管路伸入气化反应器2内底部；气化反应器2排气口与第二旋风分离器4-2进气口连通；The exhaust port of the gasification reactor 2 communicates with the air inlet of the first cyclone separator 4-1; the solid particle discharge port of the first cyclone separator 4-1 extends into the gasification reactor 2 through a pipeline Bottom; the gasification reactor 2 exhaust port communicates with the second cyclone separator 4-2 air intake;
所述第二隔离器5-2、煅烧反应器3和气化反应器2的底部，分别通过一带阀门的管路通入H2O；The bottoms of the second isolator 5-2, the calcining reactor 3 and the gasification reactor 2 are respectively fed withH2O through a pipeline with a valve;
所述空气反应器1的底部通入空气。Air is fed into the bottom of the air reactor 1 .
所述煅烧反应器3的底侧设有第二螺旋进料器6-2；气化反应器2的底侧设有第一螺旋进料器6-1。The bottom side of the calcining reactor 3 is provided with a second screw feeder 6-2; the bottom side of the gasification reactor 2 is provided with a first screw feeder 6-1.
所述气化反应器2与煅烧反应器3为鼓泡流化床；空气反应器1为快速流化床。The gasification reactor 2 and the calcining reactor 3 are bubbling fluidized beds; the air reactor 1 is a fast fluidized bed.
所述气化反应器2、煅烧反应器3、空气反应器1以及第二隔离器5-2和第一隔离器5-1的内底部分别设置有多孔布风板。The gasification reactor 2, the calcination reactor 3, the air reactor 1, and the inner bottoms of the second isolator 5-2 and the first isolator 5-1 are respectively provided with porous air distribution plates.
其实施步骤如下：Its implementation steps are as follows:
(1)设定气化反应器2恒温区温度为750℃，以赤铁矿/生石灰颗粒作为氧载体/碳载体，其活性组分为Fe2O3/CaO，并作为床料；(1) Set the temperature in the constant temperature zone of gasification reactor 2 to 750°C, use hematite/quicklime particles as the oxygen carrier/carbon carrier, and its active component is Fe2 O3 /CaO, and use it as the bed material;
(2)将生物质燃料经第一螺旋进料器6-1送入气化反应器2，在设定温度条件下发生热解反应，生成半焦、焦油以及小分子气体，其中小分子气体包括CO、H2、CO2、H2O、CH4以及少量短链烃类；水蒸汽-氧载体作为气化介质，使其中的焦油与碳氢化合物发生部分氧化重整生成CO和H2，生物质半焦主要通过水煤气反应生成CO和H2，CO通过水气变换反应与氧载体的氧化生成CO2，水蒸汽气氛下氧载体较难将H2氧化为H2O；还原的氧载体在水蒸汽气氛下部分氧化为Fe3O4，并生成H2；(2) The biomass fuel is sent into the gasification reactor 2 through the first screw feeder 6-1, and a pyrolysis reaction occurs under a set temperature condition to generate semi-coke, tar and small molecular gas, wherein the small molecular gas Including CO, H2 , CO2 , H2 O, CH4 and a small amount of short-chain hydrocarbons; water vapor-oxygen carrier is used as gasification medium to partially oxidize and reform tar and hydrocarbons to generate CO and H2 , biomass semi-coke mainly generates CO and H2 through water gas reaction, CO generates CO2 through water gas shift reaction and oxidation of oxygen carrier, it is difficult for oxygen carrier to oxidize H2 to H2 O in water vapor atmosphere; reduced oxygen The carrier is partially oxidized to Fe3 O4 under the water vapor atmosphere, and generates H2 ;
(3)床料中存在的CaO通过碳酸化反应将热解与气化反应中生成的CO2吸收，根据化学平衡原理，及时移除水煤气反应与水气反应中生成的CO2有助于平衡向生成H2的方向移动，从而促进合成气中CO向H2转化；气化反应器中的Fe2O3/CaO转化为Fe3O4/CaCO3，生物质热解产物在H2O、Fe2O3以及CaO共同作用下可生成高H2/CO比的合成气；(3) The CaO present in the bed material absorbs theCO2 generated in the pyrolysis and gasification reaction through the carbonation reaction, and according to the principle of chemical equilibrium, timely removal of theCO2 generated in the water-gas reaction and water-gas reaction contributes to the balance It moves in the direction of generating H2 , thereby promoting the conversion of CO in the syngas to H2 ; the Fe2 O3 /CaO in the gasification reactor is converted to Fe3 O4 /CaCO3 , and the biomass pyrolysis product is in H2 O , Fe2 O3 and CaO can generate syngas with high H2 /CO ratio;
(4)气化反应器2生成的合成气经过第二旋风分离器4-2的分离，将生物质灰排出，在第二旋风分离器4-2排气口得到以H2为主的合成气；反应后的固体颗粒(包括氧载体、碳载体以及残余生物质半焦)经第一隔离器5-1输送至煅烧反应器3；(4) The synthesis gas generated by the gasification reactor 2 is separated by the second cyclone separator 4-2, and the biomass ash is discharged, and the synthesis gas mainly composed ofH is obtained at the exhaust port of the second cyclone separator 4-2. gas; the reacted solid particles (including oxygen carrier, carbon carrier and residual biomass semi-coke) are transported to the calcining reactor 3 through the first separator 5-1;
(5)在煅烧反应器3中，在CO2/H2O气氛、900～950℃条件下，Fe3O4/CaCO3颗粒煅烧分解，活性组分CaO得以再生；同时将气化反应中吸收的CO2输送到第三旋风分离器4-3进行气固分离，在第三旋风分离器4-3的排气出口得到CO2/H2O混合气，并将部分CO2/H2O混合气引至煅烧反应器3底部的进气口作为流化气；(5) In the calcining reactor 3, under the condition of CO2 /H2 O atmosphere and 900-950°C, the Fe3 O4 /CaCO3 particles are calcined and decomposed, and the active component CaO is regenerated; at the same time, the The absorbed CO2 is sent to the third cyclone separator 4-3 for gas-solid separation, and the CO2 /H2 O mixed gas is obtained at the exhaust outlet of the third cyclone separator 4-3, and part of the CO2 /H2 O mixed gas is led to the gas inlet at the bottom of calcining reactor 3 as fluidizing gas;
(6)经煅烧生成的Fe3O4/CaO固体颗粒经第二隔离器5-2进入空气反应器1的底部，在900～950℃条件下与空气反应使氧载体中的晶格氧得到恢复，并由空气带出空气反应器1送至第一旋风分离器4-1；经第一旋风分离器4-1的分离，贫氧空气从第一旋风分离器(4-1)的顶部排气口排出，Fe2O3/CaO颗粒则从第一旋风分离器(4-1)底部返回到气化反应器2内，再次与生物质燃料反应。(6) The Fe3 O4 /CaO solid particles produced by calcination enter the bottom of the air reactor 1 through the second separator 5-2, and react with air at 900-950°C to obtain the lattice oxygen in the oxygen carrier Recovery, and take out air reactor 1 by air and send to the first cyclone separator 4-1; Through the separation of the first cyclone separator 4-1, the oxygen-poor air is from the top of the first cyclone separator (4-1) The Fe2 O3 /CaO particles are discharged from the exhaust port, and the Fe 2 O 3 /CaO particles return to the gasification reactor 2 from the bottom of the first cyclone separator (4-1), and react with the biomass fuel again.
如上所述，便可较好地实现本发明。As described above, the present invention can be preferably carried out.
本发明的实施方式并不受上述实施例的限制，其他任何未背离本发明的精神实质与原理下所作的改变、修饰、替代、组合、简化，均应为等效的置换方式，都包含在本发明的保护范围之内。The implementation of the present invention is not limited by the above examples, and any other changes, modifications, substitutions, combinations, and simplifications that do not deviate from the spirit and principles of the present invention should be equivalent replacement methods, and are all included in within the protection scope of the present invention.
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810019581.1ACN107974300A (en) | 2018-01-09 | 2018-01-09 | A kind of biomass chemical chain gasification method and device based on the carrier of oxygen/carbon carrier |
| PCT/CN2018/110828WO2019137056A1 (en) | 2018-01-09 | 2018-10-18 | Oxygen carrier/carbon carrier-based biomass chemical looping gasification method and device |
| ZA2020/02048AZA202002048B (en) | 2018-01-09 | 2020-05-04 | Method and device for chemical looping gasification of biomass based on an oxygen carrier/carbon carrier |
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810019581.1ACN107974300A (en) | 2018-01-09 | 2018-01-09 | A kind of biomass chemical chain gasification method and device based on the carrier of oxygen/carbon carrier |
| Publication Number | Publication Date |
|---|---|
| CN107974300Atrue CN107974300A (en) | 2018-05-01 |
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810019581.1APendingCN107974300A (en) | 2018-01-09 | 2018-01-09 | A kind of biomass chemical chain gasification method and device based on the carrier of oxygen/carbon carrier |
| Country | Link |
|---|---|
| CN (1) | CN107974300A (en) |
| WO (1) | WO2019137056A1 (en) |
| ZA (1) | ZA202002048B (en) |
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108548175A (en)* | 2018-05-30 | 2018-09-18 | 华中科技大学 | Coupling takes off the connected fluidized bed flexible feeding back device of interconnection of charcoal and atmosphere isolation |
| CN108729965A (en)* | 2018-06-08 | 2018-11-02 | 华南理工大学 | The electricity generation system and CO of the part oxygen-enriched combusting of Combined with Calcium base chain2Capture method |
| CN108822896A (en)* | 2018-06-29 | 2018-11-16 | 新奥科技发展有限公司 | A kind of gasification process and gasification installation |
| WO2019137056A1 (en)* | 2018-01-09 | 2019-07-18 | 华南理工大学 | Oxygen carrier/carbon carrier-based biomass chemical looping gasification method and device |
| CN110951508A (en)* | 2019-12-16 | 2020-04-03 | 中国科学院山西煤炭化学研究所 | A calcium oxide-based coal chemical chain catalytic gasification device and process for methane production |
| CN110964570A (en)* | 2019-12-24 | 2020-04-07 | 东南大学 | Device and method for preparing hydrogen through coal/biomass chemical chain gasification |
| CN113072981A (en)* | 2021-03-15 | 2021-07-06 | 中南大学 | Chemical chain deoxidation gasification synergistic CO for functional composite oxygen carrier2Transformation method |
| CN114275736A (en)* | 2021-11-30 | 2022-04-05 | 西安交通大学 | A chemical chain method CO2 classification regeneration process and system with red mud as oxygen carrier |
| CN114672346A (en)* | 2022-03-31 | 2022-06-28 | 华中科技大学 | Method for directly preparing carbon monoxide by using coal coke-oxygen carrier |
| CN114907884A (en)* | 2022-06-21 | 2022-08-16 | 山东省科学院能源研究所 | Multi-layer fluidized bed calcium chemical looping gasification hydrogen production device and method |
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106196027A (en)* | 2016-07-19 | 2016-12-07 | 青岛科技大学 | The multi-cell fluidized bed device that a kind of solid fuel chemistry chain converts |
| CN207828206U (en)* | 2018-01-09 | 2018-09-07 | 华南理工大学 | A kind of biomass chemical chain gasification device based on the carrier of oxygen/carbon carrier |
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20120066974A1 (en)* | 2010-09-20 | 2012-03-22 | Red Lion Bio-Energy Technologies | Tapered drum pyrolysis |
| CN103113917B (en)* | 2013-02-18 | 2014-05-14 | 上海锅炉厂有限公司 | Solid fuel chemical-looping gasification hydrogen production system and method |
| CN103113919A (en)* | 2013-03-07 | 2013-05-22 | 华北电力大学（保定） | Biomass pyrolysis system of three-stage reactor and working method thereof |
| CN106675655B (en)* | 2016-12-06 | 2019-06-11 | 西安交通大学 | A kind of biomass chemical chain gasification hydrogen production device and method based on calcium-based carbon carrier |
| CN107325846B (en)* | 2017-06-28 | 2019-10-11 | 大连理工大学 | Coal pyrolysis chemical looping gasification coupling process based on low-rank coal cascade utilization |
| CN107974300A (en)* | 2018-01-09 | 2018-05-01 | 华南理工大学 | A kind of biomass chemical chain gasification method and device based on the carrier of oxygen/carbon carrier |
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106196027A (en)* | 2016-07-19 | 2016-12-07 | 青岛科技大学 | The multi-cell fluidized bed device that a kind of solid fuel chemistry chain converts |
| CN207828206U (en)* | 2018-01-09 | 2018-09-07 | 华南理工大学 | A kind of biomass chemical chain gasification device based on the carrier of oxygen/carbon carrier |
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2019137056A1 (en)* | 2018-01-09 | 2019-07-18 | 华南理工大学 | Oxygen carrier/carbon carrier-based biomass chemical looping gasification method and device |
| CN108548175B (en)* | 2018-05-30 | 2023-09-29 | 华中科技大学 | Coupling decarbonization and atmosphere isolation interconnected fluidized bed flexible feed back device |
| CN108548175A (en)* | 2018-05-30 | 2018-09-18 | 华中科技大学 | Coupling takes off the connected fluidized bed flexible feeding back device of interconnection of charcoal and atmosphere isolation |
| CN108729965A (en)* | 2018-06-08 | 2018-11-02 | 华南理工大学 | The electricity generation system and CO of the part oxygen-enriched combusting of Combined with Calcium base chain2Capture method |
| CN108729965B (en)* | 2018-06-08 | 2023-11-03 | 华南理工大学 | Partially oxygen-enriched combustion power generation system and CO2 capture method combining calcium-based chains |
| CN108822896A (en)* | 2018-06-29 | 2018-11-16 | 新奥科技发展有限公司 | A kind of gasification process and gasification installation |
| CN110951508A (en)* | 2019-12-16 | 2020-04-03 | 中国科学院山西煤炭化学研究所 | A calcium oxide-based coal chemical chain catalytic gasification device and process for methane production |
| CN110964570B (en)* | 2019-12-24 | 2021-06-25 | 东南大学 | A device and method for preparing hydrogen by chemical chain gasification of coal/biomass |
| CN110964570A (en)* | 2019-12-24 | 2020-04-07 | 东南大学 | Device and method for preparing hydrogen through coal/biomass chemical chain gasification |
| CN113072981B (en)* | 2021-03-15 | 2022-05-24 | 中南大学 | A functional composite oxygen carrier chemical chain deoxygenation synergistic CO2 conversion method |
| CN113072981A (en)* | 2021-03-15 | 2021-07-06 | 中南大学 | Chemical chain deoxidation gasification synergistic CO for functional composite oxygen carrier2Transformation method |
| CN114275736A (en)* | 2021-11-30 | 2022-04-05 | 西安交通大学 | A chemical chain method CO2 classification regeneration process and system with red mud as oxygen carrier |
| CN114672346A (en)* | 2022-03-31 | 2022-06-28 | 华中科技大学 | Method for directly preparing carbon monoxide by using coal coke-oxygen carrier |
| CN114907884A (en)* | 2022-06-21 | 2022-08-16 | 山东省科学院能源研究所 | Multi-layer fluidized bed calcium chemical looping gasification hydrogen production device and method |
| Publication number | Publication date |
|---|---|
| ZA202002048B (en) | 2021-05-26 |
| WO2019137056A1 (en) | 2019-07-18 |
| Publication | Publication Date | Title |
|---|---|---|
| CN107974300A (en) | A kind of biomass chemical chain gasification method and device based on the carrier of oxygen/carbon carrier | |
| CN103062910B (en) | A method and device for integrating chemical looping combustion and CO2 capture | |
| CN102465047B (en) | Method for preparing methane by catalyzing and gasifying coal | |
| CN102200277B (en) | Method and device for using solid fuel chemical looping combustion | |
| CN101830432B (en) | A method and device for producing hydrogen and separating CO2 based on coal gasification | |
| CN101774542A (en) | Biomass gasification hydrogen-producing system and method | |
| CN108946661B (en) | Method and system for preparing hydrogen through biomass gasification | |
| CN108424791B (en) | Process and apparatus for synthesis gas preparation | |
| CN114574250B (en) | Method and device for preparing clean synthetic gas by biomass chemical chain gasification | |
| CN107601430B (en) | Method and device for synergistic capture of carbon dioxide based on CaFe2O4/Ca2Fe2O5 catalytic cycle for hydrogen production | |
| CN110951508A (en) | A calcium oxide-based coal chemical chain catalytic gasification device and process for methane production | |
| CN207828206U (en) | A kind of biomass chemical chain gasification device based on the carrier of oxygen/carbon carrier | |
| CN107143848A (en) | A kind of coal gasification burning chemistry chains system in situ of coupling chemistry chain oxygen | |
| CN115321478A (en) | Biomass pyrolysis chemical-looping hydrogen production device and process | |
| CN106398766B (en) | A kind of removing of enhancing chemical chain gasification hydrogen production process tar and CO2The method of trapping | |
| CN1235792C (en) | Oxygen needless hydrogen making method from solid fuel without waste gas discharging | |
| CN110982558B (en) | A method for directly producing hydrogen and carbon monoxide from coal or biomass gasification based on chemical chain technology | |
| CN103301744B (en) | A desulfurization device and method for preparing sulfur elemental particles by removing SO2 from flue gas | |
| CN115386399B (en) | Device and method for continuously preparing hydrogen based on biomass | |
| CN114955999A (en) | Biological glycerol chemical chain reforming hydrogen production CO 2 In-situ trapping and utilizing process and device thereof | |
| CN114606023A (en) | A kind of biomass negative carbon pyrolysis polygeneration system and method | |
| CN102585911A (en) | Device and method for producing hydrogen through coal gasification | |
| CN110964570B (en) | A device and method for preparing hydrogen by chemical chain gasification of coal/biomass | |
| CN103695040A (en) | Technological process for technology of preparing coal chemical chain oxygen carrier to synthesis gas | |
| CN103193202A (en) | Biomass chained circulating hydrogen production device and process |
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | Application publication date:20180501 | |
| RJ01 | Rejection of invention patent application after publication |