重整拔头油汽化技术的开发

重整拔头油由于在常温下是液体，不方便直接作为炉用燃料。开发了获国家实用新型专利的汽化器，采用汽化工艺，拔头油可代替液化气作工业窑炉燃料。工业应用试验结果表明，该轻烃燃料具有低硫、高热值的特点，与液化气相比可降低陶瓷窑的燃料费13．6％左右。该技术为炼油厂重整拔头油开辟了新的利用途径。     

热管式生物质气化炉的研究

将高温热管技术引入生物质气化中,开发了一种间接供热的热管式生物质气化炉,对高温热管的传热性能和4种生物质原料(木屑、玉米秆、稻壳和稻草)的水蒸气气化特性进行了研究。实验结果表明,气化炉内床层轴向和径向温度的变化趋势与高温热管启动温度的变化趋势基本一致。反应温度和原料种类影响气体产物的组成。在反应温度为650～950℃时,4种原料的气体产物中H2体积分数均为50%～60%,且随反应温度的升高而增加,H2含量增长率的大小顺序为:木屑>玉米秆>稻壳>稻草;CO2体积分数为15%～30%,且随反应温度的升高而减少,木屑和玉米秆的气体产物中CO2含量高于稻壳和稻草;CO和CH4含量随反应温度的升高变化较小,原料种类对CH4含量影响较小,稻壳和稻草的气体产物中CO含量比木屑和玉米秆高。     

两段炉水煤气气化工艺含酚废水的处理

两段炉水煤气气化工艺在上吹制气阶段产生含酚冷却水，下吹制氢阶段将脱除焦油，悬浮物，沉淀物并进一步过滤后的酚水加压，雾化，喷入燃烧蓄热室内与高温格子砖进行热交换，使之汽化并过热，然后与补充过热下吹蒸汽一起进入气化炉火层，酚在高温作用下分解成Ｈ２Ｏ和ＣＯ２，并进一步与炽热的炭发生反应，形成Ｈ２和ＣＯ。     

工业质谱仪在50万吨甲醇生产中的应用

美国热电的Prima dB磁扇式质谱仪的测量原理、特点及在兖矿国宏化工高硫煤年产50万吨甲醇项目中的应用情况,详细分析了与其配套的预处理系统存在的问题及改造结果。     

生物质在隔板式内循环流化床中的气化

对隔板式内循环流化床气化炉的气化特性进行了研究。考察了一些主要参变量，如温度（600～850℃）、空气当量比（0.17～0．35）和内循环率等对气化结果的影响。在实验研究的条件范围内，生物质气体产气率在1.26m^3／kg～1.9m^3／kg（标准大气压下）之间变化。气体热值在3010kJ／m^3～6195kJ／m^3（标准大气压下）范围内变化。实验结果表明，这种气化炉在750～800℃时，气化效果最好，产气率为1．7～1．9m^3／kg（标准大气压下），气体热值为6041～6195kJ／m^3之间，气化效率可达70％。     

Hydrogen-rich gas production from biomass air and oxygen/steam gasification in a downdraft gasifier

Biomass gasification is an important method to obtain renewable hydrogen. However, this technology still stagnates in a laboratory scale because of its high-energy consumption. In order to get maximum hydrogen yield and decrease energy consumption, this study applies a self-heated downdraft gasifier as the reactor and uses char as the catalyst to study the characteristics of hydrogen production from biomass gasification. Air and oxygen/steam are utilized as the gasifying agents. The experimental results indicate that compared to biomass air gasification, biomass oxygen/steam gasification improves hydrogen yield depending on the volume of downdraft gasifier, and also nearly doubles the heating value of fuel gas. The maximum lower heating value of fuel gas reaches 11.11 MJ/N m³ for biomass oxygen/steam gasification. Over the ranges of operating conditions examined, the maximum hydrogen yield reaches 45.16 g H₂/kg biomass. For biomass oxygen/steam gasification, the content of H₂ and CO reaches 63.27–72.56%, while the content of H₂ and CO gets to 52.19–63.31% for biomass air gasification. The ratio of H₂/CO for biomass oxygen/steam gasification reaches 0.70–0.90, which is lower than that of biomass air gasification, 1.06–1.27. The experimental and comparison results prove that biomass oxygen/steam gasification in a downdraft gasifier is an effective, relatively low energy consumption technology for hydrogen-rich gas production.     

论IGCC电站中气化炉型的选择

在一般论述IGCC电站对气化炉性能要求的基础上，着重比较了Texaco气化炉与Shell气化炉技术特性指标的差异，进而探讨了这两种气化炉对IGCC电站供电效率和发电成本的影响。     

彬县煤在鲁奇气化炉中的试烧

介绍了彬县煤在鲁奇气化炉中试烧的全过程.试烧结果表明,彬县煤作为鲁奇气化炉的煤源是可行的,但粗煤气出口温度、灰锁温度较高,较不易操作;相对于义马煤,租煤气中CO含量提高约5%,CH4略有降低,有效气(CO+H2)含量占61.2%.其副产物焦油、中油产率略低于义马煤.     

气化炉砌筑技术改进对施工质量的影响

本文介绍了8.53Mpa渣油型气化炉拱顶弄口炉底的砌筑改进方法,阐明其提高耐火衬里的施工质量和延长气化炉寿命的作用原理,并取得了良好的经济效益。     

An economic and energy analysis on bio-hydrogen fuel using a gasification process

Recently, in Japan, recycling technologies have been developed using waste biomass material. Waste biomass is traded in the waste materials market between users and a third-party, who receives a fee for processing them. This study is an environmental and economic analysis of a biomass energy system, which can produce hydrogen fuel for fuel cells (purity of 99.99%) as an example of an environmental business model. The experimental apparatus was made based on the moving-bed gasifier by the German company, DM2 Inc., and the hydrogen gas yield was measured. Finally, the economic viability of the future hydrogen business was estimated.The experimental results obtained gave the gas concentration of 57.5% in a Steam/Carbon ratio of 1.40 at 900 °C.Assuming the plant scale of 10 t/d, the production amount of hydrogen gas would be 21.3 kg/h. Based on the law concerning waste processing in Japan, a sizeable amount of waste biomass could be expected. Therefore, if the processing fee which is paid to the group (contractor) ranges between 5.0 and 10.0 $/t, and if the whole investment cost is 6 million dollars and the depreciation period is 15 years, the bio-hydrogen production cost using the experimental data would be 5.75–7.86 $/kg-H₂ without receiving related subsidies. In a one-third grant proportion, the cost would become 4.60–6.72 $/kg-H₂.