丙烷脱氢PtSn/Al_2O_3催化剂积炭行为研究

通过HRTEM、XRD、FT-IR、Raman、~(13)C NM R、NH_3-TPD、DTG及元素分析等表征手段,研究了丙烷脱氢PtSn催化剂积炭性质及其对催化剂结构的影响,分析了催化剂的积炭失活过程。结果表明,积炭覆盖活性位并堵塞催化剂孔道是催化剂失活主要因素;与新鲜催化剂相比,催化剂积炭完全失活后,Pt颗粒粒径并没有明显变化;完全失活时,XRD谱图出现了无定形石墨炭的衍射峰;随着积炭量的增加,焦的石墨化程度越高,芳构化程度加深,难以消除的炭增多,再生难度加大。提出丙烷在Pt活性位深度脱氢形成积炭并向载体转移的历程,认为更为稳定的C_(24)H_(12)是积炭前驱体。     

Co改性Mo/HZSM-5催化剂上甲烷无氧芳构化反应研究

甲烷无氧芳构化催化剂Ｍｏ／ＨＺＳＭ－５上担载第二组分Ｃｏ后,提高了催化剂的稳定性,但加快了催化剂上的积炭速率,且积炭速率随Ｃｏ添加量的增加而提高,因而认为催化剂的失活速率与积炭速率并不成顺比关系,研究认为,一方面,Ｃｏ的添加增加了催化剂的脱氢能力,使更多的中间产物乙烯进一步脱氢转化成芳烃或积炭,另一方面,增加了催化剂的抗积炭能力。并认为部分积炭可能对提高催化剂的稳定性起到一定的作用,空速实验表明,     

Role of hydrogen in catalytic dehydrogenation: Film diffusion controlled deactivation

The function of hydrogen used as carrier gas in catalytic dehydrogenation is to increase the selectivity and stability of catalysts. It slows down catalyst deactivation by either inhibiting deposition of potential coke precursors or facilitating their desorption by rehydrogenation. This function, in gas-solid catalytic dehydrogenation appears to be interphase mass transfer controlled by increased hydrogen linear flow velocities decreasing the extent of deactivation. Besides, deactivation appears to progress through two regimes, an initial short term followed by a long term deactivation.     

Improving the Efficiency of Dehydrogenation Catalyst Resource while Reducing the H2 Gas Circulation Rate

In the research the various ways of increasing the selectivity of the dehydrogenation process and reducing the intensity of coke formation have been studied. All results were received by means of the mathematical model of the dehydrogenation process with the calculating technique of optimal water flow. The main conclusion consists in the fact that the decrease in molar ratio H2/feed leads to increasing the catalyst deactivation by coke. It can be partially compensated by increasing the supplied water flow to the reactor to 13-14 l/h instead of 9-10 l/h at the end of cycle. Reducing the life of the catalyst to 270-290 days even at an increased water flow is determined by the intensity of the coking reactions. However, the economic feasibility of operating in such condition causes a considerable increase in production of LAB to 181-186 t/day.     

New Models of Catalyst Deactivation by Coke: II. Coking of Supported Platinum Catalysts

Metal and support deactivation upon the coking of supported metal catalysts occurs via different mechanisms. Several models of coking are presented. The most complete complex model is developed for supported platinum catalysts. It implies multilayer coke formation on support, the rapid formation of polymeric coke capable of self-regeneration by hydrogen directly in the course of reaction on platinum, and the slow conversion of this coke into graphite-like coke, which is removed only by oxidative regeneration. The models are experimentally supported for cyclohexane dehydrogenation.     

New Models of Catalyst Deactivation by Coke: I. Multilayer Coke Formation via the Consecutive Mechanism

The equations for deactivation during multilayer coke formation occurring via consecutive addition are derived. This mechanism is true for many oxide acid catalysts. The available linear and exponential relations between the activity and the coke concentration are the specific cases of these equations. The models were experimentally supported for dehydrogenation, isomerization, and reforming.     

Ferric Single-Site Catalyst Confined in a Zeolite Framework for Propane Dehydrogenation

Non-oxidative dehydrogenation of propane is a highly efficient approach for industrial preparation of propene that is commonly catalyzed by noble Pt or toxic Cr catalysts and suffers from coking. In this work, ferric catalyst confined in a zeolite framework was synthesized by a hydrothermal procedure. The isolated Fe in the framework formed distorted tetrahedra, which were beneficial for the selective dehydrogenation of propane and reached over 95 % propene selectivity and over 99 % total olefins selectivity. This catalyst had a silanol-free structure and was oxygen tolerant, hydrothermally stable, and coke free, with a deactivation constant of 0.01 h⁻¹. This study provided guidance for the synthesis of structural heteroatomic zeolite and efficient propane non-oxidative dehydrogenation over early transition metals.     

Ga2O3/HZSM-5催化剂在乙烷脱氢反应中的积碳行为和MgO的修饰作用

研究了Ga₂O₃/HZSM-5催化剂在乙烷脱氢反应中的积碳、再生以及MgO的修饰作用. 通过激光拉曼、TG-MS和NH₃-TPD等表征手段对反应过程的积碳种类和速率进行研究. 实验结果表明, 催化剂强酸中心上容易发生乙烷裂解生成甲烷的副反应并产生积碳, 其中石墨型积碳在反应过程中难以消除, 是导致催化剂失活的主要原因. MgO修饰可以减少催化剂强酸中心的量, 对乙烷裂解生成甲烷的副反应活性起到显著抑制作用, 并使积碳速率得到有效控制, 从而提高了催化剂的稳定性和乙烯的选择性. 催化剂再生时, 在空气气氛中加入水蒸气能够提高脱除石墨化碳的效率, 经420 ℃再生后催化剂的活性得到明显恢复.     

Nickel Poisoning of a Cracking Catalyst Unravelled by Single-Particle X-ray Fluorescence-Diffraction-Absorption Tomography

Ni contamination from crude oil in the fluid catalytic cracking (FCC) process is one of the primary sources of catalyst deactivation, thereby promoting dehydrogenation–hydrogenation and speeding up coke growth. Herein, single-particle X-ray fluorescence, diffraction and absorption (μXRF-μXRD-μXAS) tomography is used in combination with confocal fluorescence microscopy (CFM) after thiophene staining to spatially resolve Ni interaction with catalyst components and study zeolite degradation, including the processes of dealumination and Brønsted acid sites distribution changes. The comparison between a Ni-lean particle, exposed to hydrotreated feedstock, and a Ni-rich one, exposed to non-hydrotreated feedstock, reveals a preferential interaction of Ni, found in co-localization with Fe, with the γ-Al₂O₃ matrix, leading to the formation of spinel-type hotspots. Although both particles show similar surface zeolite degradation, the Ni-rich particle displays higher dealumination and a clear Brønsted acidity drop.     

Theoretical and Experimental Study on Reaction Coupling： Dehydrogenation of Ethylbenzene in the Presence of Carbon Dioxide

Dehydrogenation of ethylbenzene (EB) to styrene (ST) in the presence of CO2, in which EB dehydrogenation is coupled with the reverse water-gas shift (RWGS), was investigated extensively through both theoretical analysis and experimental characterization. The reaction coupling proved to be superior to the single dehydrogenation in several respects. Thermodynamic analysis suggests that equilibrium conversion of EB can be improved greatly by reaction coupling due to the simultaneous elimination of the hydrogen produced from dehydrogenation. Catalytic tests proved that iron and vanadium supported on activated carbon or Al2O3 with certain promoters are potential catalysts for this coupling process. The catalysts of iron and vanadium are different in the reaction mechanism, although ST yield is always associated with CO2 conversion over various catalysts. The two-step pathway plays an important role in the coupling process over Fe/Al2O3, while the one-step pathway dominates the reaction over V/Al2O3. Coke deposition and deep reduction of active components are the major causes of catalyst deactivation. CO2 can alleviate the catalyst deactivation effectively through preserving the active species at high valence in the coupling process, though it can not suppress the coke deposition.     

Nickel Poisoning of a Cracking Catalyst Unravelled by Single‐Particle X‐ray Fluorescence‐Diffraction‐Absorption Tomography

Ni contamination from crude oil in the fluid catalytic cracking (FCC) process is one of the primary sources of catalyst deactivation, thereby promoting dehydrogenation–hydrogenation and speeding up coke growth. Herein, single‐particle X‐ray fluorescence, diffraction and absorption (μXRF‐μXRD‐μXAS) tomography is used in combination with confocal fluorescence microscopy (CFM) after thiophene staining to spatially resolve Ni interaction with catalyst components and study zeolite degradation, including the processes of dealumination and Brønsted acid sites distribution changes. The comparison between a Ni‐lean particle, exposed to hydrotreated feedstock, and a Ni‐rich one, exposed to non‐hydrotreated feedstock, reveals a preferential interaction of Ni, found in co‐localization with Fe, with the γ‐Al₂O₃ matrix, leading to the formation of spinel‐type hotspots. Although both particles show similar surface zeolite degradation, the Ni‐rich particle displays higher dealumination and a clear Brønsted acidity drop.     

焦油催化裂化催化剂积炭失活的实验研究

对白云石、石灰石作用下生物质热解焦油催化裂化过程中的积炭失活问题进行了研究，考察了较长反应时间内催化剂积炭量和焦油转化率的变化情况。最长运行时间32 h，所得积炭质量分数为3%～15%，焦油转化率下降到70％左右。对不同来源焦油的生焦性、催化裂化反应条件等对积炭形成的影响作了考察，并从动力学角度对催化活性与积炭量之间的关系进行了分析，得到了单层积炭和多层积炭阶段线性和指数形式的关联式。     

甲醇制烯烃反应过程中SAPO-34催化剂积炭动力学研究

在固定床反应器中研究了甲醇制烯烃反应过程中SAPO-34分子筛催化剂的积炭动力学,分别得到了催化剂积炭量与反应温度、剂醇比的经验关联式。结果表明,催化剂床层存在明显的积炭分布,在450 ℃,甲醇WHSV为15 h－1,催化剂积炭量随催化剂反应运行时间（Time on Stream, TOS）为25 min时,床层入口处的积炭量平均为9.56%,而出口处的积炭量平均为3.20%,属于平行失活,积炭主要来源于甲醇生成的高碳中间体,这些中间体在生成低碳烃的同时生成积炭。从积炭的生成机理出发,得到了SAPO-34分子筛催化剂的积炭动力学机理模型,将催化剂积炭量与一定催化剂停留时间内反应过程中甲醇的转化量相关联,该模型形式同样简单,能够较好地拟合实验数据。     

Hydrogen Effect on Coke Removal and Catalytic Performance in Pre-Carburization and Methane Dehydro-Aromatization Reaction on Mo/HZSM-5

1. Introduction As an effective utilization of methane, the methane dehydro-aromatization was focused in the last decade [1-28]. Over the Mo/HZSM-5 bi- functional catalyst at high reaction temperature, methane can be converted into light aromatics (ben- zene and naphthalene) and hydrogen. Mo active species can activate the C—H bond of methane; and HZSM-5 supplies the acid sites for the oligomeriza- tion and cyclization of hydrocarbons to form aromat- ics, and suppresses the deeper condens…     

多相催化体系的反应机理和失活模式(英文)

Solving the problem of catalyst deactivation is essential in process design. To do this, various aspects of the kinetics of processes with catalyst deactivation, and their different mechanisms, are discussed. Catalyst deactivation often cannot be avoided, but more knowledge on its mechanism can help to find kinetic means to reduce its harmful consequences. When deactivation is caused by coke, the generation of coke precursors is the determining step in the deactivation kinetics. Different types of deactivation were distinguished that lead to different evolution of the process. The phenomenon of non-uniform coking can be linked to catalyst surface non-uniformity. For the class of catalysts with more than one type of active sites, an explanation was suggested for the observed trends in the deactivation modes. For catalytic proc-esses using catalyst particles of industrial size, the influence of intraparticle diffusion resistance is important. The analysis showed that for a number of processes, the decrease of the reaction rate due to deactivation is less under diffusion control. For certain reaction mechanisms, there exist operation conditions where the rate of the process under diffusion control exceeds the rate in the kinetic control regime. A signifi-cant problem is the change of selectivity in the course of catalyst deactivation. The selectivity may either decrease or increase, and depends on the reaction mechanism during deactivation. The changes are larger when there is no diffusion resistance. The intentional poisoning of catalysts and its influence on catalyst activity and selectivity for the process of ethylene oxide production was discussed.     

Deactivation of Molybdenum-Containing Zeolites in the Course of Nonoxidative Methane Conversion

It was found that the nonoxidative dehydroaromatization of methane occurs over Mo-containing pentasil-type zeolites with various framework compositions at 750°C. This reaction is accompanied by catalyst deactivation because of coke formation. The effects of the space velocity of methane and the composition of the zeolite matrix on the amount and properties of the resulting condensation products were studied. It was found that the lowest amount of coke with a relatively low degree of polycondensation was formed on zeolite with SiO₂/Al₂O₃ = 40 containing Mo nanoparticles.     

Ni/Al~2O~3催化剂上CH~4分解生成的碳物种的转化

本文利用顺序脉冲实验技术,对CH~4在Ni/Al~2O~3催化剂上分解生成的碳物种及其在实验条件下的转化行为进行研究,以探索催化剂上积炭形成的原因。     

Role of silica-alumina catalyst texture in the reaction of propane oxidative dehydrogenation in the presence of sulfur dioxide

The effects of preparation conditions, component ratio, and pretreatment temperature (1000–1550‡C) of silica-alumina samples on their phase composition, texture characteristics, and catalytic properties are studied in the reaction of the oxidative dehydrogenation of propane by sulfur dioxide. It is shown that the samples contain individual silicon and aluminum oxides. The product of their interaction (mullite) is formed only at 1550°C. Mesoporous and macroporous catalysts with monoand polydispersed pore distributions over sizes are obtained. It is found that the porous structure of the catalyst plays a key role in the process of the oxidative dehydrogenation of propane in the presence of sulfur dioxide at 600–700°C. The apparent rate of propylene formation increases with an increase in the pore volume with radii between 10 and 100 nm. Propane is transformed into propylene more selectively on the catalyst where the pores with radii of 10–100 nm dominate; narrower pores (< 10 nm) are favorable for the formation of coke and complete oxidation products.     

Ga2O3催化剂上CO2气氛中丙烷脱氢反应的研究

考察了Ga2O3对于丙烷脱氢和CO2气氛脱氢反应的催化性能,结果表明,Ga2O3具有较高的催化活性,其性能优于传统的Cr2O3脱氢催化剂,催化反应可能经过了一个丙烷异裂的过程,其中CO2是通过逆水煤气反应和Boudouard反应来促进催化剂性能的,在高于823K时该促进作用更为明显,催化剂的催化活性和其表面酸密度密切相关,在Ga2O3结构中,四配位Ga^3＋是其酸位的来源,并通过质子与氧化物的共同作用促进反应进行,催化剂的失活是由于表面的积碳和活性氧的消耗共同造成的,同时还对Ga2O3作为丙烷脱氢反应的催化剂的催化反应机理进行了初步探讨。     

Rod-shaped porous alumina-supported Cr2O3 catalyst with low acidity for propane dehydrogenation

Direct catalytic propane dehydrogenation (PDH) to obtain propylene is a more economical and environmentally friendly route for propylene production. In particular, alumina-supported Cr₂O₃ catalysts can have better potential applications if the acidic properties could be tuned. Herein, a series of rod-shaped porous alumina were prepared through a hydrothermal route, followed by calcination. It was found that the acidity of the synthesized alumina was generally lower than that of the commercial alumina and could be adjusted well by varying the calcination temperature. Such alumina materials were used as supports for active Cr₂O₃, and the obtained catalysts could enhance the resistance to coke formation associated with similar activity in PDH reaction compared to the commercial alumina. The amount of coke deposited on a self-made catalyst (Cr-Al-800) was 3.6%, which was much lower than that deposited on the reference catalyst (15.7%). The lower acidity of the catalyst inhibited the side reactions and coke formation during the PDH process, which was beneficial for its high activity and superior anti-coking properties.