Kinetic study of propane dehydrogenation and catalyst deactivation over Pt-Sn/Al2O3 catalyst

The kinetics of propane dehydrogenation and catalyst deactivation over Pt-Sn/Al2O3 catalyst were studied.Performance test runs were carried out in a fixed-bed integral reactor.Using a power-law rate expression for the surface reaction kinetics and independent law for deactivation kinetics,the experimental data were analyzed both by integral and a novel differential method of analysis and the results were compared.To avoid fluctuation of time-derivatives of conversion required for differential analysis,the conversion-time data were first fitted with appropriate functions.While the time-zero and rate constant of reaction were largely insensitive to the function employed,the rate constant of deactivation was much more sensitive to the function form.The advantage of the proposed differential method,however,is that the integration of the rate expression is not necessary which otherwise could be complicated or impossible.It was also found that the reaction is not limited by external and internal mass transfer limitations,implying that the employed kinetics could be considered as intrinsic ones.     

Effect of mass transfer limitations on catalyst performance during reduction and carburization of iron based Fischer-Tropsch synthesis catalysts

Existence of intraparticle mass transfer limitations under typical Fischer-Tropsch synthesis has been reported previously,but there is no suitable study on the existence of intraparticle diffusion limitations under pretreatment steps (reduction and activation) and their effect on catalytic performance for iron based catalysts.In this study,Fe-Cu-La-SiO2 catalysts were prepared by co-precipitation method.To investigate the intraparticle mass transfer limitation under reduction,activation and reaction steps,and its effect on catalytic performance,catalyst pellets with different sizes of 6,3,1 and 0.5 mm have been prepared.All catalysts were calcined,pretreated and tested under similar conditions.The catalysts were activated in hydrogen (5%H2in N2) at 450℃ for 3 h and exposed to syngas (H2/CO=1) at 270℃ and atmospheric pressure for 40 h.Afterwards,FTS reaction tests were performed for approximately 120 h to reach steady state conditions at 290℃,17 bar and a feed flow (syngas H2/CO=1) rate of 3 L/h (STP).Using small pellets resulted in higher CO conversion,FT reaction rate and C5+ productivity as compared with larger pellets.The small pellets reached steady state conditions just 20 h after starting the reaction.Whereas for larger pellets,CO conversion,FT reaction rate and C5+ productivity increased gradually,and reached steady state and maximum values after 120 h of operation.The results illustrate that mass transfer limitations exist not only for FTS reaction but also for the reduction and carburization steps which lead to various phase formation through catalyst activation.Also the results indicate that some effects of mass transfer limitations in activation step,can be compensated in the reaction step.The results can be used for better design of iron based catalyst to improve the process economy.     

Stability and activity of carbon nanofiber-supported catalysts in the aqueous phase reforming of ethylene glycol

Nickel, cobalt, copper and platinum nanoparticles supported on carbon nano-fibers were evaluated with respect to their stability, catalytic activity and selectivity in the aqueous phase reforming of ethylene glycol (230 C, autogenous pressure, batch reactor). The initial surface-specific activities for ethylene glycol reforming were in a similar range but decreased in the order of Pt (15.5 h1 ) >Co(13.0 h1 ) >Ni(5.2 h1 ) while the Cu catalyst only showed low dehydrogenation activity. The hydrogen molar selectivity decreased in the order of Pt (53%)>Co(21%)>Ni (15%) as a result of the production of methane over the latter two catalysts. Over the Co catalyst acids were formed in the liquid phase while alcohols were formed over Ni and Pt. Due to the low pH of the reaction mixture, especially in the case of Co (as a result of the formed acids), significant cobalt leaching occurs which resulted in a rapid deactivation of this catalyst. Investigations of the spent catalysts with various techniques showed that metal particle growth is responsible for the deactivation of the Pt and Ni catalysts. In addition, coking might also contribute to the deactivation of the Ni catalyst.     

Direct conversion of natural gas to higher hydrocarbons:A review

Direct conversion of methane to higher hydrocarbons is an effective process to solve the problem of natural gas utilization. Although remarkable progress has been achieved on the dehydro-aromatization of methane (DAM), low conversion caused by severe thermodynamic limitations,coke formation, and catalysis deactivation remain important drawbacks to the direct conversion process. Molybdenum catalysts supported on HZSM-5 type zeolite support are among the most promising catalysts. This review focuses on the aspects of direct methane conversion, in terms of catalysts containing metal and support, reaction conditions, and conversion in different types of reactors. The reaction mechanism for this catalytic process is also discussed.     

Insight into the topology effect on the diffusion of ethene and propene in zeolites: A molecular dynamics simulation study

Selectivity control is a difficult scientific and industrial challenge in methanol-to-olefins(MTO)conversion.It has been experimentally established that the topology of zeolite catalysts influenced the distribution of products.Besides the topology effect on reaction kinetics,the topology influences the diffusion of reactants and products in catalysts as well.In this work,by using COMPASS force-field molecular dynamics method,we investigated the intracrystalline diffusion of ethene and propene in four different zeolites,CHA,MFI,BEA and FAU,at different temperatures.The self-diffusion coefficients and diffusion activation barriers were calculated.A strong restriction on the diffusion of propene in CHA was observed because the self-diffusion coefficient ratio of ethene to propene is larger than 18 and the diffusion activation barrier of propene is more than 20 kJ/mol in CHA.This ratio decreases with the increase of temperature in the four investigated zeolites.The shape selectivity on products from diffusion perspective can provide some implications on the understanding of the selectivity difference between HSAPO-34 and HZSM-5 catalysts for the MTO conversion.     

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.     

Weakening internal diffusion effect in selective hydrodesulfurization of FCC gasoline by novel designed eggshell CoMoS/Al2O3 catalysts

A simple method for preparation of presulfided eggshell CoMoS/γ-Al2O3 catalysts with sharp boundary is developed, through which the eggshell thicknesses of Co and Mo could be easily regulated by controlling the impregnation time. According to the results characterized by EDS, XRD, HRTEM and FT-IR of adsorbed CO, the active component structures, the nature and/or the amount of active sites on the eggshell catalyst are similar to these on the uniform catalyst. The evaluation results of the catalytic performance in selective hydrodesulfurization (HDS) of FCC gasoline show the presence of significant internal diffusion inhibition effect on HDS of S-compounds especially in the uniform catalyst. Compared with uniform catalyst, the eggshell catalyst could remarkably reduce such an internal diffusion inhibition effect due to a shortened diffusion path of the reactants, thus showing higher HDS activity and selectivity.     

Study on Ni/C catalysts for vapor phase carbonylation of ethanol

Activated carbon-supported Ni catalysts for vapor phase carbonylation of ethanol to propionic acid in the presence of ethyl iodide as promoter were investigated. Under optimum reaction conditions, the conversions of carbon monoxide and ethanol were measured to be 81.4% and 98.4%, respectively, while the selectivity for propionic acid was found to be 98.65%. The catalyst was stable within 48 h on stream. XRD and XPS methods were used to characterize the structures and surface properties of the fresh and tested catalysts. The characterization results indicated that aggregation of nickel particles and formation of nickel iodide on the catalyst surface should be responsible for the deactivation of the catalysts.     

Effects of Temperature and Catalyst to Oil Weight Ratio on the Catalytic Conversion of Heavy Oil to Propylene Using ZSM-5 and USY Catalysts

It is useful for practical operation to study the rules of production of propylene by the catalytic conversion of heavy oil in FCC (fluid catalytic cracking). The effects of temperature and C/O ratio (catalyst to oil weight ratio) on the distribution of the product and the yield of propylene were investigated on a micro reactor unit with two model catalysts, namely ZSM-5/Al2O3 and USY/Al2O3, and Fushun vacuum gas oil (VGO) was used as the feedstock. The conversion of heavy oil over ZSM-5 catalyst can be comparable to that of USY catalyst at high temperature and high C/O ratio. The rate of conversion of heavy oil using the ZSM-5 equilibrium catalyst is lower compared with the USY equilibrium catalyst under the general FCC conditions and this can be attributed to the poor steam ability of the ZSM-5 equilibrium catalyst. The difference in pore topologies of USY and ZSM-5 is the reason why the principal products for the above two catalysts is different, namely gasoline and liquid petroleum gas (LPG), repspectively. So the LPG selectivity, especially the propylene selectivity, may decline if USY is added into the FCC catalyst for maximizing the production of propylene. Increasing the C/O ratio is the most economical method for the increase of LPG yield than the increase of the temperature of the two model catalysts, because the loss of light oil is less in the former case. There is an inverse correlation between HTC (hydrogen transfer coefficient) and the yield of propylene, and restricting the hydrogen transfer reaction is the more important measure in increasing the yield of propylene of the ZSM-5 catalyst. The ethylene yield of ZSM-5/Al2O3 is higher, but the gaseous side products with low value are not enhanced when ZSM-5 catalyst is used. Moreover, for LPG and the end products, dry gas and coke, their ranges of reaction conditions to which their yields are dependent are different, and that of end products is more severe than that of LPG. So it is clear that maximizing LPG and propylene and restricting dry gas and coke can be both achieved via increasing the severity of reaction conditions among the range of reaction conditions which LPG yield is sensitive to.     

Are Solid Catalysts Successfully Emulating Enzymes?

 In many aspects, similitude exists between man-made catalysts and enzymes. Can scientific insight into this similitude stimulate new research directions in catalysis? More precisely, can the understanding of the mechanisms of activity control in enzymes suggest new advances for man-made catalysts? Indeed, it is already possible to design catalysts with (i) new structures (e.g. presence of several phases) and (ii) a better balance between the roles of the different components. The ambition is to keep the essential advantages of solids as catalysts, in particular robustness, easy separation from products, and tolerance to high temperatures, while adding the advantages typical of enzymes, like more activity, allostery, and more precise control of selectivity, in particular enantioselectivity. The ambition is to build a bridge between robust man-made functional solids and fragile but extremely selective enzymes. For that, results from a line of the work in our group will be used.     

不同条件下苯与丙烯烷基化反应的催化剂失活研究

对不同条件下苯与丙烯烷基化反应Hβ催化剂的寿命、失活催化剂的积炭量和积炭性质进行了研究。在5.7MPa下，随反应温度变化，反应介质在反应过程中所经历的相态变化不同，导致催化剂的寿命、失活催化剂的积炭量和积炭的性质也存在着较大差异。300℃时，反应介质处于接近于体系临界点的超临界相或高压液相状态，催化剂寿命最长，积炭量大。失活催化剂积炭的元素分析及TPO-MS表征结果发现，积炭的碳氢比与反应温度有关，温度越高，碳氢比越高；而积炭的脱炭温度与反应时间（催化剂寿命）相关，催化剂寿命越长，相应的脱炭温度也越高。     

水对V2O5/AC催化剂低温还原NO的影响

 研究了烟气中的水对新型V2O5／AC催化剂选择催化还原NO的影响．结果表明,水通过与反应物（如NO和NH3）的竞争吸附而在一定程度上降低了催化剂的活性．在SO2共存下,水的存在导致硫酸铵盐在催化剂表面的过量沉积,造成催化剂孔道堵塞,比表面积减小,从而使催化剂失活．较高的反应温度（如553K）和／或低空速有利于催化剂的活性和稳定性．脱除活性焦载体中的矿物质可在一定程度上减缓催化剂失活的速率,但不能完全抑制水对V2O5／AC催化剂的毒化作用．     

Kinetic Models of Catalyst Deactivation in Paraffin Dehydrogenation

The results of studying the deactivation of both unpromoted platinum–alumina catalysts and those promoted with K, Li, In, Sn, and W in the dehydrogenation of lower and higher paraffins are discussed. The main reason for catalyst deactivation is found to be coke formation. The rate laws of coke formation and paraffin dehydrogenation in the non-steady-state regime of the reaction are derived. The catalyst sulfuring is found to enhance its stability. The effects of oxygen and water impurities on the reactions and coke formation are studied.     

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。     

Mo基分子筛催化剂及甲烷无氧芳构化

本文综述了甲烷无氧芳构化反应及Mo基分子筛催化剂的研究进展。在众多的催化剂中以Mo基分子筛催化性能最佳。概括了催化剂中关于MoO_<em>x前躯体结构和其在分子筛中落位,Mo₂C物种和诱导期等;讨论了反应中涉及的中间产物、双功能机理以及催化剂失活等问题;归纳了催化剂制备过程中制备方法、焙烧温度与时间、Mo载量和分子筛硅铝比以及催化剂预处理对反应活性的影响;综述了提高催化剂催化性能和反应性能的各种方法,并对其分析,同时介绍了两种催化剂再生方法。最后,依据本实验室研究进展,对甲烷芳构化从工艺角度进行一些可行性讨论,并提出相关问题和展望。     

邻苯二酚与乙醇单醚化反应用固体酸催化剂表面上的积炭行为

 研究了邻苯二酚与乙醇气固相单醚化反应用固体酸催化剂表面上的积炭行为，并用TG－DTA，BET，GC－MS，FT－IR和元素分析等手段对积炭物种进行了表征．结果表明，催化剂上有两种类型的积炭，一类属可溶性积炭，主要由二苯醚及其衍生物组成，可在低温燃烧除去；另一类属不可溶性积炭，主要为缺氢的芳烃类聚合物或类石墨碳，需在高温下才能烧除．积炭主要发生在4～8nm范围的中孔内，导致反应后的催化剂大孔范围的孔分布所占的分数增大．随着反应的进行，总积炭量逐渐增多．     

干气制乙苯结炭沸石催化剂烧炭再生研究

以苯和炼厂干气中的乙烯合成乙苯结炭催化剂为研究对象，对结炭催化剂上积炭的性质及不同温度下的烧炭情况进行了研究，考察了再生前后催化剂的酸性、活性、晶相、比表面及孔结构等性能的变化。结果表明，催化剂孔的内表面积炭占据了酸性中心，致使催化剂活性降低；在烧炭时温度大于300 ℃才开始烧炭，最佳烧炭温度应控制在500℃～550℃，600 ℃可将炭完全烧净。程序升温脱附（TPD）实验表明，550 ℃实验室烧炭后催化剂酸种类及其比例可完全恢复，酸量可恢复到95%。晶相、孔结构基本未变，催化剂的活性得到良好恢复。     

合成气一步法制备液化石油气单管实验研究

采用甲醇合成催化剂与脱水催化剂机械混合,制备了液化石油气(LPG)合成催化剂。以模拟生物质气为原料气,在固定床单管实验装置上,温度(220~330 ℃)、压力(1.2~5.1 MPa)和空速(500~3 000 h^-1)条件下考察催化剂的性能。结果表明,在325 ℃、2.1 MPa、1 500 h^-1条件下,CO转化率达到72.36%,LPG占烃类产物的71.21%。当设定温度为325 ℃、压力2.1 MPa时、空速≤2 500 h^-1时,系统可以稳定运行;空速达到3 000 h^-1时,反应器内部温度迅速升高无法控制,造成催化剂烧结失活。针对上述催化剂,采用NH₃-TPD、XRD、N₂吸附-脱附和TPO对催化剂进行了表征。结果表明,催化剂的积炭、强酸位酸性降低及比表面积的降低是导致催化剂活性降低的重要影响因素。     

SO_4~(2-)促进型多元氧化物超强酸催化剂上丁烷异构化反应

考察了一系列SO促进型多元氧化物超强酸催化剂的正丁烷异构化反应性能．在ZrO2中添加Ni、Fe、Cr、Mn和V等第二和第三组份金属元素可有效地提高催化剂在氮气气氛下的异构化活性，但催化剂活性下降很快．改成氢气气氛可使部分多元氧化物催化剂的积炭速度减缓，进一步提高活性和稳定性．载铂对提高SO／ZrO2催化剂的活性和稳定性是有效的，但对多元氧化物催化剂无积极作用．在临氢反应过程中，添加的金属元素价态未发生变化，催化剂的稳定性与积炭量相对应，烧炭以后初活性可完全恢复，积炭可能是造成催化剂迅速失活的主要原因．     

Catalytic cracking of polyethylene over nanocrystalline HZSM-5: Catalyst deactivation and regeneration study

In this work, catalytic cracking of low density polyethylene (LDPE) over nanocrystalline HZSM-5 zeolite in a batch reactor at 340 °C was carried out with the aim of study both the catalyst resistance to deactivation and the catalyst regeneration process. For looking into the catalyst deactivation, consecutive polyethylene cracking experiments were carried out. Subsequently, the same reactions has been also performed but by regenerating the zeolite after each experiment by promoting coke combustion at 550 °C under air flow. Zeolites used were two samples of nanocrystalline HZSM-5 with very different textural properties (sample A, with most of its surface corresponding to zeolitic micropores and sample B with a considerable amount of external surface, mesopores and super-micropores) in order to study the effect of their textural properties in the deactivation and regeneration experiments. Although conversion and activity values reached over both samples are quite high taking into account the mild conditions used, sample B shows a very much higher initial activity than A due to its improved textural properties. In both samples two different deactivation mechanisms occur: a reversible deactivation by coke deposition removable by the regeneration procedure, and an irreversible or permanent deactivation by other factors. Deactivation of sample B occurs faster due to the higher amount of coke deposited on this material. However, the improved textural properties of this catalyst supposes an advantage for the regeneration process, since coke deposited either on the external surface or on the super-micropores and mesopores, makes easier the regeneration procedure.