齐鲁石化公司研究院最新科技成果信息报道

甲醇合成催化剂 保护剂实现国产化 (王冬梅 周广林 ) 齐鲁石化公司研究院最新科技成果信息报道 　　甲醇合成催化剂保护剂能有效地脱除原料气中羰基铁、镍，延长甲醇合成催化剂寿命，降低粗甲醇中的杂质含量，具有精脱硫剂和脱除羰基铁、镍的双重功能。由齐鲁石化公司研究院研制开发的 QXJ－ 01和 QMG－ 01甲醇合成催化剂保护剂分别于 2000年和 2001年在齐鲁石化第一化肥厂 10万吨 /年甲醇上实现国产化，综合性能分别达到德国南方化学公司的 K306和丹麦托普索公司的 MG901水平。 轴径向变换反应器实现国产化 (王玉珍 王毓秀 ) 齐鲁石化…     

甲醇合成催化剂保护剂实现国产化

甲醇合成催化剂保护剂能有效地脱除原料气中羰基铁、镍,延长甲醇合成催化剂寿命,降低粗甲醇中的杂质含量,具有精脱硫剂和脱除羰基铁、镍的双重功能。由齐鲁石化公司研究院研制开发的 QXJ－ 01和 QMG－ 01甲醇合成催化剂保护剂分别于 2000年和 2001年在齐鲁石化第二化肥厂 100 kt/a甲醇上实现国产化,综合性能分别达到德国南方化学公司的 K306和丹麦托普索公司的 MG901水平。甲醇合成催化剂保护剂实现国产化@王冬梅 @周广林     

甲醇合成催化剂保护剂实现国产化

甲醇合成催化剂保护剂能有效地脱除原料气中羰基铁、镍 ,延长甲醇合成催化剂寿命 ,降低粗甲醇中的杂质含量 ,具有精脱硫剂和脱除羰基铁、镍的双重功能。由齐鲁石化公司研究院研制开发的 QXJ- 0 1和 QMG- 0 1甲醇合成催化剂保护剂分别于 2 0 0 0年和 2 0 0 1年在齐鲁石化第二化肥厂 10万t/ a甲醇上实现国产化 ,综合性能分别达到德国南方化学公司的 K30 6和丹麦托普索公司的 MG90 1水平甲醇合成催化剂保护剂实现国产化@王冬梅 @周广林     

甲醇合成催化剂保护剂实现国产化

甲醇合成催化剂保护剂能有效地脱除原料气中羰基铁、镍 ,延长甲醇合成催化剂寿命 ,降低粗甲醇中的杂质含量 ,具有精脱硫剂和脱除羰基铁、镍的双重功能。由齐鲁石化公司研究院研制开发的ＱＸＪ - 0 1和ＱＭＧ - 0 1甲醇合成催化剂保护剂分别于 2 0 0 0年和 2 0 0 1年在齐鲁石化第二化肥厂 10万吨 /年甲醇上实现国产化 ,综合性能分别达到德国南方化学公司的Ｋ30 6和丹麦托普索公司的ＭＧ90 1水平。甲醇合成催化剂保护剂实现国产化@王冬梅 @周广林     

甲醇合成催化剂保护剂实现国产化

甲醇合成催化剂保护剂能有效地脱除原料气中羰基铁、镍、延长甲醇合成催化剂寿命 ,降低粗甲醇中的杂质含量 ,具有精脱硫剂和脱除羰基铁、镍的双重功能。由齐鲁石化公司研究院研制开发的ＱＸＪ - 0 1和ＱＭＧ - 0 1甲醇合成催化剂保护剂分别于 2 0 0 0年和 2 0 0 1年在齐鲁石化第二化肥厂 10万吨 /年甲醇上实现国产化 ,综合性能分别达到德国南方化学公司的Ｋ30 6和丹麦托普索公司的ＭＧ90 1水平甲醇合成催化剂保护剂实现国产化@王冬梅 @周广林     

甲醇合成催化剂保护剂实现国产化

甲醇合成催化剂保护剂能有效地脱除原料气中羰基铁、镍、延长甲醇合成催化剂寿命 ,降低粗甲醇中的杂质含量 ,具有精脱硫剂和脱除羰基铁、镍的双重功能。由齐鲁石化公司研究院研制开发的ＱＸＪ - 0 1和ＱＭＧ - 0 1甲醇合成催化剂保护剂分别于 2 0 0 0年和 2 0 0 1年在齐鲁石化第二化肥厂 1 0万吨 /年甲醇上实现国产化 ,综合性能分别达到德国南方化学公司的Ｋ30 6丹麦托普索公司的ＭＧ90 1水平。甲醇合成催化剂保护剂实现国产化@王冬梅 @周广林     

甲醇合成催化剂保护剂实现国产化

甲醇合成催化剂保护剂能有效地脱除原料气中羰基铁、镍 ,延长甲醇合成催化剂寿命 ,降低粗甲醇中的杂质含量 ,具有精脱硫剂和脱除羰基铁、镍的双重功能。由齐鲁石化公司研究院研制开发的ＱＸＪ— 0 1和ＱＭＧ— 0 1甲醇合成催化剂保护剂分别于 2 0 0 0年和 2 0 0 1年在齐鲁石化第二化肥厂10万ｔ/ａ甲醇上实现国产化 ,综合性能分别达到德国南方化学公司的Ｋ30 6和丹麦托普索公司的ＭＧ90 1水平。甲醇合成催化剂保护剂实现国产化     

齐鲁石化公司研究院最新科技成果信息

甲醇合成催化剂保护剂实现国产化甲醇合成催化剂保护剂能有效地脱除原料气中羰基铁、镍 ,延长甲醇合成催化剂寿命 ,降低粗甲醇中的杂质含量 ,具有精脱硫剂和脱除羰基铁、镍的双重功能。由齐鲁石化公司研究院研制开发的ＱＸＪ -０１和ＱＭＧ -０１甲醇合成催化剂保护剂在齐鲁石化第二化肥厂１０万ｔ／ａ甲醇上实现国产化 ,综合性能分别达到德国南方化学公司的Ｋ３０６和丹麦托普素公司的ＭＧ９０１水平。（王冬梅周广林）轴径向变换反应器实现国产化轴径向变换反应器由瑞士卡萨尔公司首先实现工业化 ,在中国已有４个变换反应器采用了该技术 ,…     

齐鲁石化公司研究院最新科技成果信息

甲醇合成催化剂保护剂实现国产化　甲醇合成催化剂保护剂能有效地脱除原料气中羰基铁、镍 ,延长甲醇合成催化剂寿命 ,降低粗甲醇中的杂质含量 ,具有精脱硫剂和脱除羰基铁、镍的双重功能。由齐鲁石化公司研究院研制开发的ＱＸＪ 0 1和ＱＭＧ 0 1甲醇合成催化剂保护剂分别于 2 0 0 0年和 2 0 0 1年在齐鲁石化第二化肥厂 1 0 0ｋｔ/ａ甲醇上实现国产化 ,综合性能分别达到德国南方化学公司的Ｋ30 6和丹麦托普索公司的ＭＧ90 1水平轴径向变换反应器实现国产化　轴径向变换反应器由瑞士卡萨利公司首先实现工业化 ,在中国已有 4个变换反应器采用了…     

成果集锦

甲醇合成催化剂保护剂实现国产化甲醇合成催化剂保护剂能有效地脱除原料气中羰基铁、镍 ,延长甲醇合成催化剂寿命 ,降低粗甲醇中的杂质含量 ,具有精脱硫剂和脱除羰基铁、镍的双重功能。由齐鲁石化公司研究院研制开发的ＱＸＪ- 0 1和ＱＭＧ - 0 1甲醇合成催化剂保护剂分别于 2 0 0 0年和 2 0 0 1年在齐鲁石化第二化肥厂 1 0万吨 /年甲醇上实现国产化 ,综合性能分别达到德国南方化学公司的Ｋ30 6和丹麦托普索公司的ＭＧ90 1水平。(王冬梅 ,周广林 )轴径向变换反应器实现国产化轴径向变换反应器由瑞士卡萨尔公司首先实现工业化 ,在中国已有 4个…     

A novel microfabricated Pd/SiO2 model catalyst for the hydrogenation of 1,3-butadiene

The hydrogenation of 1,3-butadiene was successfully demonstrated using a microfabricated catalyst. The reaction was carried out at atmospheric pressure and 100°C with a hydrogen to hydrocarbon ratio of 125. Data from a thin film Pd/silica catalyst is also presented for comparison. The conversion for the microfabricated catalyst is more stable and slightly lower than that for the thin film catalyst; however, the geometric surface area of the thin film catalyst is 7.5 times greater than that of the microfabricated catalyst. The selectivity of the reaction products is greatly different between the two catalysts. The microfabricated catalyst has a much lower selectivity for 1-butene and favors the 2-butenes more so than does the thin film catalyst.     

HC-402-2型苯加氢均相催化剂的研究

HC-402-2型催化剂为四组分苯加氢均相催化剂.第一组分为有机酸镍(主催化剂),第二组分为烷基铝(助催化剂),由上述两组分构成的催化剂属于原子态金属催化剂,其活性极不稳定,反应周期(寿命)很短。在原子态金属催化剂的基础上,评选出了最佳配位体第三组分,研制成功金属配位体催化剂,其活性稳定性和反应周期与原子态金属催化剂相比较有极大改善,使反应周期大大增长。同时还发现了第四组分促进剂,使催化剂的活性明显提高,反应速度明显加快。HC-402-2型催化剂的开发应用提高了装置的安全、技术水平和经济效益。     

Optimization of the reactor–regenerator system with catalytic parallel–consecutive reactions

The system with moving deactivating catalyst, composed of a cocurrent tubular reactor and a catalyst regenerator with an additional flux of a fresh catalyst, has been investigated. For the temperature dependent catalyst deactivation, the optimization problem has been formulated in which a maximum of a process profit flux is achieved by a best choice of temperature profile along tubular reactor, best catalyst recycle ratio and best catalyst activity after regeneration. The set of parallel–consecutive reactions, A+B→R and R+B→S, with desired product R has been taken into account. A relatively unknown, powerful discrete algorithm in which a suitably defined Hamiltonian is constant along the optimal path, has been applied for optimization. The optimal solutions have been discussed. In particular, it has been shown that an increase of the unit cost of catalyst regeneration or an increase of the catalyst recycle ratio causes such optimal temperatures in reactor which save the catalyst, as the optimal temperature profiles are then shifted towards lower temperatures. Finally these profiles reach isothermal shape at the level of minimum allowable temperature and then there is no further possibility to control the reactor process by the temperature profile. Thus the catalyst activity after regeneration, as well as an average catalyst activity in the reactor do decrease when the unit catalyst regeneration cost increases. This is a new form of catalyst saving, as the catalyst deactivation rate becomes reduced when an average catalyst activity is allowed to decrease. It is important that this form of catalyst saving appears in the region where any saving of the catalyst by an optimal choice of temperature profile is impossible. It has been also shown that for small values of the catalyst recycle ratio, the catalyst regenerator should be removed from the system. In such a case, the renewal of catalyst takes place due to a fresh catalyst input, exclusively.     

Optimal temperature profiles for parallel-consecutive reactions with deactivating catalyst

A cocurrent tubular reactor with temperature profile control and recycle of moving deactivating catalyst has been investigated. For the temperature-dependent catalyst deactivation, the optimization problem has been formulated in which a maximum of a profit flux is achieved by the best choice of temperature profile and residence time of reactants for the set of catalytic reactions A+B→R and R+B→S with desired product R, the rates of reactions have been described separately for every reagent by the expressions containing (temperature dependent) reaction rate constants, concentrations of reagents, catalyst activity, as well as catalyst concentration in the reacting suspension and a measure of the slip between reagents and solid catalyst particles. The algorithms of maximum principle have been used for optimization. The optimal solutions show that a shape of the optimal temperature profile depends on the mutual relations between activation energies of reactions and catalyst deactivation. It has been proved that the optimal temperature profile is a result of the compromise between the overall production rate of desired reagent R (production rate in the first reaction minus disappearance rate in the second one), necessity of saving of reagents residence time (reactor volume) and necessity of saving catalyst; the most important influence on the optimal temperature profile is associated with necessity of saving the catalyst. When catalyst recycle ratio increases (mean number of catalyst particles residing in reactor increases), optimal temperatures save the catalyst, as the optimal profile is shifted in direction of lower temperatures. The same is observed when catalyst slip increases (catalyst residence time in reactor increases). Despite of variation in the catalyst concentration the optimal profile is practically the same because the decay rate is affected only by instantaneous activity of catalyst. When reactor unit volume price decreases, catalyst residence time increases, whereas optimal temperature profile is shifted to lower temperatures. When economic value of unit activity of outlet catalyst increases (catalyst with a residual activity still has an economic value), catalyst saving should be more and more intense. As far as possible, the optimal profile is shifted in direction of lower temperatures, whereas the optimal residence time is still the same. Then the optimal profile is isothermal at the level of minimum allowable temperature, whereas the catalyst is saved as its residence time in reactor decreases.     

烯醛一步法合成异戊二烯Ag—P催化剂的研制

本文介绍了Ag——P催化剂的研制过程,考查了周期表中一些元素的催化活性,并确定了催化剂成份和适宜的制备条件,其中包括催化剂的氨处理和载体扩孔等,其选择性高于Cr—P催化剂。     

外齿轮形颗粒催化剂上乙烯催化氧化的反应工程计算

针对乙烯氧化制环氧乙烷反应体系,对外齿轮异形催化剂建立三维反应-传质-传热模型。有效扩散系数和有效热导率均为待求解浓度场和温度场的函数,使得偏微分方程组模型为强非线性。采用有限元算法求解,并对模型有效性进行验证,定量研究了催化剂几何比外表面积和内扩散效率因子的关系。计算结果表明,几何比外表面积为1862 m²·m^-3的外齿轮催化剂内扩散效率因子为0.1804,而几何比外表面积为924 m²·m^-3的圆柱形催化剂内扩散效率因子为0.0993。对单个催化剂颗粒反应-传递现象的研究能定量指导催化剂设计,并为耦合反应器流体力学和催化剂反应传递现象多尺度模拟计算奠定基础。     

OPTIMUM REACTOR DESIGN IN METHANATION PROCESSES WITH NONUNIFORM CATALYSTS

A generic methodology is developed to design a heterogeneous catalytic reactor for methanation processes. For the optimization of a heterogeneous catalytic reactor, nonuniform catalyst pellets such as a layered catalyst are considered with respect to reaction type, reactor performance, and component distribution inside the catalyst. Heterogeneous uniform and nonuniform catalyst models were developed to analyze the effect of mass and heat transfer between both bulk phase and catalyst surface and inside a catalyst pellet. Then, concentration profiles of hydrogen and carbon monoxide in the catalyst pellet and along the reactor axis were obtained by analyzing simulation results. It was shown that the application of different types of nonuniform catalyst pellets at a certain number of separate zones within a reactor could produce higher catalyst performance than a reactor with uniform catalyst. Furthermore, it proved a significant decrease of catalyst deactivation behavior such as coking and sintering. Layered catalysts were optimized to maximize an overall reactor performance over the catalyst lifetime, achieving capital cost reduction characterized by reactor size, catalyst amount, and degree of catalyst deactivation. Last, temperature control throughout the reactor operating periods was strategically planned for a reactor operation with distribution of nonuniform catalyst pellets. This methodology can also be usefully applied to the design of heterogeneous catalytic reactors for other processes such as hydro-treating process and cracking process.     

碳二前加氢催化剂的应用

采用均匀设计方法,进行了碳二前加氢催化剂的制备,确定了催化剂的最佳配方和制备工艺。1000h工业侧线对比评价结果表明,自制催化剂活性稍低于市售催化剂,选择性高于市售催化剂,两种催化剂总体性能相当。X光电子能谱分析表明,自制催化剂钯银合金作用更为明显,X荧光光谱分析表明表面活性组分含量低于市售催化剂。     

Optimal inlet temperature control of reactors with catalyst decay

The constant conversion policy which has been shown to be optimal in certain classes of optimal control problems for reactors with decaying catalyst is examined here for the inlet temperature control in a tubular reactor where the catalyst decay is a function of the composition. A single irreversible reaction is considered where the rate expression is a product of separate functions of temperature, concentration or conversion and catalyst activity. The catalyst decay rate expression is also a product of separate functions of the same variables. A proof of the constant exit conversion property is given for problems where the decay rate is of first-order with respect to the catalyst activity.     

SCR催化剂技术研究进展及专利技术分析

介绍了SCR催化剂的相关技术,SCR催化剂技术的国内外专利申请有3个申请高峰,目前已处于第三个申请高峰的上升阶段。SCR催化剂技术申请人国外主要为企业,我国主要是高校,申请专利量占我国申请人申请专利总量的50%以上。催化剂功效主要是提高催化剂的耐受性和活性,约占统计样本数量的22%和52%。通过配方技术提高功效的申请量达到906件,约占统计样本的78%。技术创新仍以SCR催化剂配方及提高催化剂活性稳定为研究热点,但不能忽略对催化剂材料、催化剂再生技术和降低催化剂成本等研究,开发出适合我国国情的具有自主知识产权的SCR催化剂成套技术。