低温加氢催化剂的设计：理论与实践(英文)
多晶硅中英文词汇
多晶硅工程中英文词汇参考安全淋浴safety shower安全生产safety production安全数据safety data安全有效运行safe and efficient operation按照工艺要求加工硅芯seed rod processing to process requirements.板坯slab办公室office room半导体级别semiconductor grade半导体级多晶硅polycrystalline silicon for semi-conductor purpose包装packing包装间packaging room报警alarm泵的液压计算pump hydraulic calculations必须的设计标准necessary design criteria必需的公用设施required utilities必需的公用设施和消耗率required utilities and consumption rates避免聚合物在下游工艺过程中在非常条件下进行反应而发生爆炸to avoid explosion of the polymer in downstream processes by reacting it under very controlled conditions 编制安全阀和其它安全装置清单prepare a list of safety valve and other safety devices编制设备说明书prepare equipment specifications编制以下仪表设计数据prepare instrument design data including the following变配电站substation and power distribution station标准编码standard label标准参数standard parameter标准设备规格specification of standard equipment标准设备装置的规格specifications for standard equipment set表面分析surface analysis表面金属total surface metals表压（磅/平方英寸）psig,不断循环continuous cycling不理想to be non-ideal不锈钢stainless steel布袋收尘器bag house, bag house filter部件编码和位置item number with location操作程序operating procedures操作和维修最大负荷表table of maximum operating and maintenance loads操作人员和工程师培训operators and engineers training操作数据operating data操作顺序operating sequence操作条件operating conditions操作要严谨确保安全must be completed in a precise manner for safetyreasons.产出/投入比input and output ratio产量production capacity产品products产品规格product specifications产品检测product examination产品库product storage产品流product stream产品浓度计算product concentration产品质量quality of product常规晶棒regular rod厂房和/或构筑物的特殊要求special requirements for buildings and/or structures厂区管网pipeline network within the plant area厂区设施plant area facilities厂区占地面积occupied area of the plant area超高纯水ultrapure water超高纯水水池ultrapure water bath彻底清洁最终产品completely clean up the final product称量weighing城市管道水水质的分析指数analytical index of water quality for city water pipe network程序procedures充足的技术信息sufficient technical information抽气evacuations出口outlet出炉的多晶硅棒process harvested polysilicon rods初步布置平面图preliminary arrangement plans初始洗涤initial scrubber储放区holding area储罐场tank storage farm储液槽storage tank处理厂treatment plant传达室gate house传导性conductivity传热流体heat transfer fluid串联的池室consecutive bath chamber纯度purity纯度合格的三氯氢硅desired purities of TSC纯度合格的四氯化硅desired purities of STC纯净水purified water纯品储罐pure storage tank纯三氯氢硅pure TCS纯三氯氢硅储罐pure TCS holding tank纯三氯氢硅罐pure-TCS tank纯三氯氢硅加料罐pure TCS feed head tank纯水pure water纯四氯化硅pure STC粗三氯氢硅储罐crude TCS tank催化剂catalysts带旋流器的备用氯化炉standby chlorinator with the cyclone袋装冶金硅tote bag me-Si单晶硅方棒single crystal silicon square ingot单晶硅头尾料nose and tail material of single crystal silicon单晶及硅片加工车间single crystal silicon and silicon wafer processing plant 单晶拉制monocrystal pulling单线图one-line diagram道路road低成本太阳能用硅low-cost silicon for solar battery purpose低能洗涤器low energy imparting scrubber低能中和系统low energy imparting neutralization system低品位三氯氢硅low grade TCS低热值Lower heating value低温低压氯化工艺low temperature and pressure chlorination process低压lower voltage低压氯化法low pressure chlorination process底馏分塔bottom cut tower电极夹具electrode holder电价electricity price电流加热heated by electrical current电气设计electrical design电阻率resistivity调节到合格点to be controlled at a desired point调压阀pressure control valve (PCV)动作action独立的洗涤器装置separate scrubber unit钝化处理passivation treatment。
加氢反应器的设计要求和结构分析
一.设计背景工程科学是关于工程实践的科学基础，现代过程装备与控制工程是工程科学的一个分支，因此，生产实习是工科学习的重要环节。
在兰州兰石集团实习期间，对化工设备的发展前景和各种化工容器如反应釜、换热器、储罐、分液器和塔器等的有所了解和学习。
生产实习的主要任务是学习化工设备的制造工艺和生产流程，将理论知识与生产实践相结合，理论应用于实际。
因此，过程装备与检测的课程设计的设置是十分必要的。
由于我们实习的加工车间正在进行加氢反应器的生产，而加氢反应器是石油化工行业的关键设备，其生产工艺和设计制造在化工设备中具有显著的代表性，为此，选择加氢反应器这一典型的化工设备作为课程设计的设计题目。
二加氢反应器的主要设计参数2.1：引用的主要标准及规范国家质量技术监督局颁发的《压力容器安全技术监察规程》（99）版GB150-1998 《钢制压力容器》GB6654-1996 压力容器用钢板（含1、2号修改单）JB4708-2000 钢制压力容器焊接工艺评定JB/T4709-2000 钢制压力容器焊接规程JB4744-2000 钢制压力容器产品焊接试板的力学性能检验JB/T4730-2005 承压设备无损检测JB4726-2000 压力容器用碳素钢和低合金钢锻件JB4728-2000 压力容器用不锈钢锻件GB/4237-2007 不锈钢热轧钢板和钢带GB/T3280-2007 不锈钢冷轧钢板和钢带GB/T3077-1999 合金结构钢GB/T14976-2002 流体输送用不锈钢无缝钢管JB/T4711-2003 压力容器涂敷与运输包装2.2 主要技术参数表一设计压力8.4MPa设计温度400℃最高工作压力7.8MPa最高工作温度343℃容器类别三类容器容积225立方米腐蚀裕量 5水压试验立式7.47／卧式7.55MPa盛装介质石脑油、油气、氢气、硫化氢主体材质 2.25Cr-1Mo2.3 结构特点该加氢精制反应器为板焊结构，其内径φ4000㎜，壁厚96.5㎜，由2节组成；封头内半径2043.5㎜，壁厚96.5㎜，总重量94550Kg。
应用化学专业英语翻译(第二版)
Unit10 Nomenclature of Hydrocarbons碳氢化合物的命名Alkanes烷烃理想的，每一种化合物都应该由一个明确描述它的结构的名称，并且通过这一名称能够画出它的结构式。
为了这一目的，全世界的化学家接受了世界纯粹与应用化学会（IUPAC）建立的一系列规则。
这个系统就是IUPAC系统，或称为日内瓦系统，因为IUPAC的第一次会议是在瑞士日内瓦召开的。
不含支链的烷烃的IUPAC命名包括两部分（1）表明链中碳原子数目的前缀；（2）后缀－ane，表明化合物是烷烃。
用于表示1至20个碳原子的前缀见表10.1表10.1中前4个前缀是由IUPAC选择的，因为它们早已在有机化学中确定了。
实际上，它们甚至早在它们成为规则之下的结构理论的暗示之前，它们的地位就确定了。
例如，在丁酸中出现的前缀but－，一种表示在白脱脂中存在的四个碳原子的化合物（拉丁语butyrum白脱（黄油））。
表示5个或更多碳原子的词根来源于希腊或拉丁词根。
含取代基的烷烃的IUPAC名称由母体名称和取代基名称组成，母体名称代表化合物的最长碳链，取代基名称代表连接在主链上的基团。
来源于烷烃的取代基称为烷基。
字母R－被广泛用来表示烷烃的存在.烷烃的命名是去掉原烷基名称中的－ane加上后缀－yl。
例如，烷基CH3CH2－称为乙基。
CH3－CH3乙烷（原碳氢化合物）CH3CH2－乙基（一个烷基）下面是IUPAC的烷烃命名规则：1. 饱和碳氢化合物称为烷烃。
2. 对有支链的碳氢化合物，最长的碳链作为主链，IUPAC命名按此主链命名。
3. 连接在主链上的基团称为取代基。
每一取代基有一名称和一数字.这一数字表示取代基连接在主链上的碳原子的位置。
4. 如果有多于一个的相同取代基，要给出表示支链位置的每个数字。
而且，表示支链数目的数字由前缀di－，tri－，tetra－，penta－等表示。
5. 如果有一个取代基，主链碳原子编号从靠近支链的一端开始，使支链位号最小。
氢能电解槽英语术语
氢能电解槽英语术语English Answer：Hydrogen Electrolyzer Terminology.Anode: The electrode in an electrolyzer where oxidation occurs and hydrogen gas is produced.Cathode: The electrode in an electrolyzer where reduction occurs and oxygen gas is produced.Electrolyte: The conductive medium between the anode and cathode that allows the flow of ions.Electrolyzer: A device that uses electricity to split water into hydrogen and oxygen gases.Hydrogen Production Rate (HPR): The rate at which hydrogen gas is produced by an electrolyzer, typically measured in kilograms per hour (kg/h).Alkaline Electrolyzer: An electrolyzer that uses an alkaline electrolyte, such as potassium hydroxide (KOH).Anion Exchange Membrane (AEM) Electrolyzer: An electrolyzer that uses an anion exchange membrane as the electrolyte.Balance of Plant (BOP): The auxiliary equipment and systems that support the operation of an electrolyzer, such as water treatment, gas compressors, and power conditioning.Current Density: The amount of current passing through the electrolyzer per unit area of the electrode, typically measured in amperes per square centimeter (A/cm2).Depolarization: The reduction of the overpotential required for hydrogen evolution, which increases the efficiency of the electrolyzer.Efficiency: The ratio of the amount of energy required to produce hydrogen to the amount of energy stored in thehydrogen gas produced.Electrolysis: The process of using electricity to decompose water into hydrogen and oxygen gases.Faradaic Efficiency: The ratio of the actual amount of hydrogen produced to the theoretical amount that should be produced based on the amount of electricity used.Hydrogen Generation Unit (HGU): A system that combines an electrolyzer with auxiliary equipment, such as water treatment, gas compressors, and power conditioning.Ion Exchange Membrane (IEM) Electrolyzer: An electrolyzer that uses an ion exchange membrane as the electrolyte.Operating Voltage: The voltage required to drive the electrolysis reaction in an electrolyzer.Oxygen Production Rate (OPR): The rate at which oxygen gas is produced by an electrolyzer, typically measured inkilograms per hour (kg/h).Proton Exchange Membrane (PEM) Electrolyzer: An electrolyzer that uses a proton exchange membrane as the electrolyte.Stack: A series of electrolyzer cells connected electrically in series.Thermodynamic Efficiency: The ratio of the maximum possible amount of energy that can be stored in the hydrogen produced to the amount of electricity required to produce it.Water Splitting: The process of splitting water into hydrogen and oxygen gases using electrolysis.中文回答：氢能电解槽术语。
加氢催化剂、加氢反应器基础知识
加氢催化剂、加氢反应器基础知识概述加氢精制催化剂是由活性组分、助剂和载体组成的。
其作用是加氢脱除硫、氮、氧和重金属以及多环芳烃加氢饱和。
该过程原料的分子结构变化不大，，根据各种需要，伴随有加氢裂化反应，但转化深度不深，转化率一般在10%左右。
加氢精制催化剂需要加氢和氢解双功能，而氢解所需的酸度要求不高。
工作原理催化加氢的机理(改变反应途径，降低活化能)：吸附在催化剂上的氢分子生成活泼的氢原子与被催化剂削弱了键的烯、炔加成。
(1)双键碳原子上烷基越多，氢化热越低，烯烃越稳定：R2C=CR2 > R2C=CHR > R2C=CH2 > RCH=CH2 > CH2=CH2(2)反式异构体比顺式稳定(3)乙炔氢化热为-313.8kJ·mol－1，比乙烯的两倍（-274.4kJ·mol－1）大，故乙炔稳定性小于乙烯。
应用在Pt、Pd、Ni等催化剂存在下，烯烃和炔烃与氢进行加成反应，生成相应的烷烃，并放出热量，称为氢化热(heat of hydrogenation，1mol不饱和烃氢化时放出热量)。
催化加氢的机理（改变反应途径，降低活化能）：吸附在催化剂上的氢分子生成活泼的氢原子与被催化剂削弱了键的烯、炔加成。
分类1、加氢裂化催化剂加氢裂化催化剂（hydrocracking catalyst）是石油炼制过程中，重油在360~450℃高温，15~18MPa高压下进行加氢裂化反应，转化成气体、汽油、喷气燃料、柴油等产品的加氢裂化过程使用的催化剂。
加氢裂化过程在石油炼制过程属于二次加工过程，加工原料为重质馏分油，也可以是常压渣油和减压渣油，加氢裂化过程的主要特点是生产灵活性大，产品的分布可由操作条件来控制，可以生产汽油、低凝固点的喷气燃料和柴油，也可以大量生产尾油用作裂解原料或生产润滑油。
所得的产品稳定性好，但汽油的辛烷值不高，。
由于操作条件苛刻，设备投资和操作费用高，应用不如催化裂化广泛。
The field of heterogeneous catalysis中文翻译
Rational Design of Low-Temperature Hydrogenation Catalysts:Theoretical Predictions and Experimental Verification低温加氢催化剂的设计: 理论与实践The field of heterogeneous catalysis, specifically catalysis on bimetallic alloys, has seen many advances over the past few decades. One of the main goals of the catalysis industry is to develop new materials that have novel catalytic properties. Bimetallic catalysts, which often show electronic and chemical properties that are distinctly different from those of the parent metals, offer the opportunity to design new catalytic materials with enhanced activity, selectivity, and stability [1-2] . Currently bimetallic catalysts are widely utilized in many heterogeneous catalysis [3] and electro-catalysis [4] applications.In order to understand the origins of the novel catalytic properties, bimetallic surfaces have been the subject of many experimental and theoretical studies, as summarized in several reviews [5-7] . It is now well established that bimetallic surfaces often show novel properties that are not present on either of the parent metal surfaces [5-16] . The modification effect is especially important when the admetal coverage is in the sub monolayer to monolayer regime. However, it is difficult to know a priori how the electronic and chemical properties of a particular bimetallic surface will be modified relative to the parent metals. For this reason, the study of bimetallic surfaces in the field of catalysis has gained considerable interest. There are two critical factors that contribute to the modification of the electronic and chemical properties of a metal in a bimetallic surface. First, the formation of the hetero-atom bonds changes the electronic environment of the metal surface, giving rise to modifications of its electronic structure through the ligand effect. Second, the geometry of the bimetallic structure is typically different from that of the parent metals, e.g. the average metal-metal bond lengths change. This lattice mismatch leads to the strain effect that is known to modify the electronic structure of the metal through changes in orbital overlap [16] . While studies on model bimetallic surfaces provide fundamental insights into the novel properties, in an industrially relevant supported catalyst the active metal will be present in the form of nanoparticles. As shown in Fig.1, research efforts in our group involve three parallel approaches, with the goals being to bridge the“materials gap”and“pressure gap”between fundamental surface science studies and real world catalysis. In the current review we will utilize hydrogenation reactions as examples to demonstrate how the utilization of these three parallel approaches can lead to the rational design of bimetallic catalysts with novel low-temperature hydrogenation activities.Catalytic hydrogenations are among the most commonly practiced catalytic processes, ranging from common steps in organic synthesis, to batch processes in pharmaceutical production, to stabilization of edible oils, and to petroleum upgrading processes. Because hydrogenation reactions are typically exothermic, it is advantageous to carry out these reactions at low temperatures. In the current review we will first use the hydrogenation of cyclohexene to demonstrate the feasibility of increasing the low-temperature hydrogenation activity by reducing the binding energies of atomic hydrogen and cyclohexene, which can be achieved by designing bimetallic surfaces with specific surface structures. We will then discuss several other types of hydrogenation reactions to further illustrate the advantages of bimetallic catalysts in terms of both hydrogenation activity and selectivity.1 Structures of bimetallic surfacesIn the current review we will focus mainly on bimetallic surfaces by depositing one monolayer ofa 3d transition metal on either a Pt(111) single crystal or a polycrystalline Pt substrate. As shown in Fig.2, monolayer bimetallic surfaces can have three ideal configurations: a surface 3d-Pt-Pt(111) configuration, where the 3d monolayer grows epitaxially on the surface of the Pt substrate; an intermixed configuration, where the 3d atoms reside in the first two Pt layers to some varying degree; and the unique subsurface Pt-3d-Pt(111) configuration, where the first layer is comprised of Pt atoms and the second layer is occupied with the 3d metals.Procedures for the preparation of bimetallic surface structures under ultra-high vacuum (UHV) conditions have been described in detail previously [5] . For example, the Ni/Pt(111) bimetallic surfaces have been characterized using a wide range of experimental techniques and DFT modeling [17] . When Ni is deposited with the Pt(111) surface held at 300 K, Ni atoms stay on the top-most layer to produce the Ni-Pt-Pt(111) surface configuration. If this surface is subsequently heated to 600 K, or if the monolayer deposition of Ni occurs with the Pt(111) substrate held at 600 K, most of the Ni atoms diffuse into the subsurface region to produce the Pt-Ni-Pt(111) subsurface structure. Similar surface and subsurface structures have been obtained for several other 3d metals on the Pt(111) substrate [5,18] .The ab initio calculations in the current review were performed using the Vienna Ab initio Simulation Package (V ASP) version 4.6 [19-20] . The monolayer bimetallic systems were modeled on the closed-packed Pt(111) substrate. The PW91 functional was used within the generalized gradient approximation with an energy cutoff on the basis set of 396 eV. The bimetallic systems were modeled using a periodic 2*2 or 3*3 unit cell with four metal layers, with the slabs being separated by 6 equivalent layers of vacuum in the epitaxial direction. The top two layers were allowed to relax to the lowest energy configuration while the third and fourth layers were frozen at the bulk Pt-Pt distance. More details about the DFT modeling procedures on monolayer bimetallic surfaces can be found in a recent review [5] .2 Low-temperature hydrogenation of cyclohexeneCyclohexene is used as a probe molecule to study the hydrogenation because cyclic hydrocarbons are important reaction intermediates in many refinery and petrochemical processes, in addition to serving as building blocks for many chemicals produced in the chemical industry. Furthermore, cyclohexene has several competitive reaction pathways, including decomposition, dehydrogenation, disproportionation (self-hydrogenation), and hydrogenation. Comparative studies of these reaction pathways provide an opportunity to determine how the hydrogenation activity and selectivity are affected by the formation of bimetallic surfaces.2.1 DFT and experimental studies on single crystal surfacesOne hypothesis for promoting the low-temperature hydrogenation of alkene is that both reactants, atomic hydrogen and alkene, should bond relatively weakly on the catalyst surface to facilitate the hydrogenation steps. DFT calculations were performed to estimate the values of hydrogen binding energy (HBE) on several 3d-Pt-Pt(111) and Pt-3d-Pt(111) surfaces, as shown in Fig.3A [18] . Fig.3A reveals that HBE is related to the position of the surface d-band center with respect to the Fermi level, in agreement with the trend observed in previous studies for other surfaces [5] . In general, the addition of a 3d metal surface layer on Pt(111)moves the d-band center closer to the Fermi level as compared to the bulk 3d metals. This is primarily due to the tensile strain induced by the Pt lattice as the ligand effect is the weakest between late transition metal over layers and the Pt(111) substrate [17] . Conversely, subsurface 3d metals shift the surface d-band center of Pt away from the Fermi level as compared to that of Pt(111), mainly due to the electronic interactionof Pt and the subsurface 3d atoms [17] . The comparison in Fig.3A demonstrates that HBE typically follows the trend of 3d-Pt-Pt(111)>Pt(111)> Pt-3d-Pt(111). In addition, the nearly linear correlation between HBE and the surface d-band center should enable one to predict HBE on other bimetallic surfaces based on the extensive database of d-band center values for many bimetallic surfaces [5] .In addition to the trend in the correlation of HBE with surface d-band center, the binding energies of unsaturated hydrocarbons, such as cyclohexene, follows the same trend as HBE. As shown in Fig.3B, DFT calculations reveal that the Pt-3d-Pt(111) subsurface structures bond to cyclohexene more weakly than Pt(111) and the corresponding 3d-Pt-Pt(111) surface structures [18] . For example, DFT results indicate that both cyclohexene and atomic hydrogen are more weakly bonded on Pt-Ni-Pt(111) than on Ni-Pt-Pt(111), Pt(111) and Ni(111), suggesting that the subsurface Pt-Ni-Pt(111) structure should be more effective in the hydrogenation of cyclohexene than the surface structure. This has been confirmed experimentally by comparing the hydrogenation activity of cyclohexene using temperature programmed desorption (TPD), as shown in Fig.4 [18] . As illustrated in the TPD peak area of the cyclohexane product, the subsurface Pt-Ni-Pt (111) structure shows the highest hydrogenation yield, with the desorption peak centered at a very low temperature of 203 K. Similar bimetallic surface structure can also be produced by depositing one monolayer of Pt on a Ni(111) substrate, which also possesses the novel low-temperature pathway for cyclohexene hydrogenation [21] .The trend in the DFT calculations in Fig.3B also shows that the binding energy of cyclohexene on Pt-Co-Pt(111) and Pt-Fe-Pt(111) is even weaker than that on Pt-Ni-Pt(111). Although this might suggest that the former two surfaces would be more active toward the hydrogenation than Pt-Ni-Pt(111), one should keep in mind that the adsorption of cyclohexene needs to be strong enough for the hydrogenation to take place. One would therefore expect to observe a volcano relationship for the hydrogenation activity as the d-band center moves further away from the Fermi level, i.e., when the adsorption of cyclohexene becomes too weak for the hydrogenation to occur. This is verified experimentally in the results shown in Fig.5. The hydrogenation yield from TPD measurements is the highest on Pt-Ni-Pt(111), but starts to decrease on the Pt-Co-Pt(111) and Pt-Fe-Pt(111) surfaces, where the binding of cyclohexene becomes too weak for hydrogenation to occur. On the other side of the volcano curve, the binding energies of cyclohexene on the 3d-Pt-Pt(111) surfaces are too strong, preventing the effective hydrogenation of cyclohexene [18] 2.2 Polycrystalline bimetallic surfacesIndustrial catalysts are often supported nanoparticles of varying shape and size. Polycrystalline bimetallic films provide a potential way to bridge the “materials gap”between single crystal surfaces and supported catalysts. As illustrated in Fig.6, it is possible to assume that the surface chemistry of the nanoparticle should be dominated primarily by the first few atomic layers. It is also reasonable to assume that the chemistry of the individual crystal facets on the nanoparticle (primarily (111) and (100) for an FCC nanoparticle) can be approximated by their respective single crystal extension [22] .With these assumptions we have investigated the chemical properties of 3d-Pt bimetallic structures prepared on a polycrystalline Pt film that contained mainly the (111) and (100) facets. Similar to Pt(111), monolayer Ni was deposit on a Pt foil at room temperature to produce the Ni-Pt-Pt surface structure, followed by annealing to higher temperatures to obtain the Pt-Ni-Pt subsurface structure [22] . The TPD results of the hydrogenation of cyclohexene are shown inFig.7. Similar to the corresponding single crystal surfaces, the subsurface Pt-Ni-Pt polycrystalline structure shows significantly higher hydrogenation activity than that from the polycrystalline Pt and Ni surfaces. These results confirm the assumption that the trend observed on single crystal bimetallic surfaces can be extended to the polycrystalline counterparts.2.3 Thermodynamic stability of bimetallic surfaces under hydrogenation conditionsBefore extending the surface science results to supported catalysts, it is important to verify that the desirable Pt-Ni-Pt subsurface structure is the thermodynamically preferred configuration under hydrogenation conditions. As demonstrated in several recent studies, including single crystal surfaces [23-24] , polycrystalline films [22,25] and supported catalysts [26] , the thermodynamically preferred Pt-Ni bimetallic structure is directly related to the chemical environment present on the surface. Fig.8 shows the DFT predicted potential for segregation for a 3d metal atom to segregate from the subsurface to the surface of Pt(111). These values were calculated for the environments of vacuum, and with 0.5 monolayer (ML) atomic hydrogen and 0.5 ML atomic oxygen, using procedures described previously [24] . The thermodynamic potential for segregation is defined as follows:where ΔE seg is the thermodynamic potential for segregation per Pt-3d pair, E A/3d-Pt-Pt is the total energy for the surface configuration with adsorbate A, E A/Pt-3d-Pt is the total energy for the subsurface configuration with adsorbate A, and M is the total number of Pt-3d pairs per unit cell. As defined in a previous publication [22] , a positive ΔE seg value indicates that the subsurface Pt-3d-Pt is more stable. The DFT results in Fig.8 predict that for the reducing environment of vacuum and 0.5 ML atomic hydrogen, the subsurface configuration is thermodynamically preferred, whereas in 0.5 ML atomic oxygen the surface configuration is preferred. There is a nearly linear trend between ΔE seg and the difference in d-band, ΔƐd , which leads to a generalized equation in predicting the thermodynamic stability of a wide range of bimetallic surfaces [24] . Because the environment of hydrogenation reactions is similar to that of the reducing environment, with the bimetallic surface being partially covered by hydrogen, the results in Fig.8 suggest that the desirable subsurface Pt-Ni-Pt configuration should be thermodynamically stable, making it possible to extend model surfaces to supported catalysts for hydrogenation reactions.2.4 Synthesis and evaluation of supported catalystsSupported monometallic Pt and bimetallic Ni-Pt and Co-Pt catalysts were synthesized on γ-Al 2 O 3 using the incipient wetness method [27-28] . The catalysts were characterized using a variety of techniques, including extended X-ray absorption fine structure (EXAFS). The utilization of EXAFS is critical in these studies because it provides direct information on the extent of bimetallic bond formation based on the coordination numbers of Ni-Pt and Co-Pt under in-situ reaction conditions. As summarized in Table 1, the detection of the Ni-Pt and Co-Pt nearest neighbors confirms that bimetallic bonds are indeed produced on the supported catalysts [28] . The supported catalysts were evaluated using both batch and flow reactors to determine the reaction kinetics of the hydrogenation of cyclohexene at a low temperature of 303 K [28] . Fig.9 shows the production of cyclohexane from cyclohexene on Pt/γ-Al 2 O 3 , Co-Pt/γ-Al 2 O 3 , and Ni-Pt/γ-Al 2 O 3 , using a batch reactor equipped with Fourier transform infrared (FTIR)spectroscopy. The solid lines are fittings using the Langmuir-Hinshelwood model, resulting in a rate constant of 1.7, 21 and 24 min -1 for supported Pt, Co-Pt, and Ni-Pt, respectively [28] . The trend observed in the rate constant of cyclohexene hydrogenation is consistent with that from the single crystal surfaces for the same reaction, Ni-Pt>Co-Pt>Pt, as shown earlier in the volcano curve in Fig.5. The observation of the similar trend between model surfaces and supported catalysts provides an important demonstration of the rational design of bimetallic catalysts from combined theoretical and experimental approaches.3 Research opportunities in bimetallic catalysis3.1 Low-temperature hydrogenation reactionsWe have applied similar combined approaches for the design of bimetallic catalysts for the low-temperature hydrogenation of several types of hydrocarbon molecules. Below we will provide several examples of hydrogenation reactions that are of both fundamental and practical importance.Hydrogenation of acrolein. Studies of the selective hydrogenation of unsaturated aldehydes, such as αβ-unsaturated aldehydes, have been of growing interest for the production of fine chemical sand pharmaceutical precursors [29] .The hydrogenation of the C=C and/or C=O bonds in unsaturated aldehydes offers the possibility to improve both the hydrogenation activity and selectivity through the formation of bimetallic surfaces. Using the hydrogenation of acrolein as a probe reaction, we demonstrated that the selective hydrogenation of the C=O bond can be achieved through the formation of the subsurface Pt-Ni-Pt(111) and Pt-Co-Pt(111) bimetallic structures [30-31] .Hydrogenation of benzene.The hydrogenation of benzene to cyclohexane is of significant importance in the petroleum industry and for environmental protection. The process of benzene hydrogenation has been utilized commercially for the production of cyclohexane, which is one of the key intermediates in the synthesis of Nylon-6 and Nylon-66 [32] . We have identified Co-Pt bimetallic catalysts as promising materials for the hydrogenation of benzene at a relatively low temperature of 343 K [28,33] . For example, Table 2 summarizes the batch and flow reactor results of benzene hydrogenation on several Co-based bimetallic catalysts. The Co-Pt catalyst shows the highest rate constant and lowest activation barrier for the hydrogenation of benzene, which is consistent with the relatively weak binding energies of atomic hydrogen and benzene from DFT calculations [33] . In addition, the catalyst support also plays a role in controlling the hydrogenation activity of Co-Pt catalysts [34]Selective hydrogenation of acetylene in ethylene. The selective hydrogenation of acetylene in the presence of ethylene is an important reaction because acetylene poisons the catalysts in ethylene polymerization reactions [35-36] . By supporting Pd-Ag bimetallic catalysts on ion-exchanged β-zeolites, we observed a synergistic effect that led to a higher selectivity for acetylene hydrogenation in the presence of excess ethylene [37] .The increase in the hydrogenation selectivity is attributed to a combination of an enhanced π-cation interaction between acetylene and zeolite at low temperatures and the ability of the Pd-Ag bimetallic catalysts to perform hydrogenation at such low temperatures [37] .3.2 Reducing bulk Pt in bimetallic catalysts with metal carbidesAs demonstrated in Figs.3-5, the subsurface Pt-Ni-Pt structure is desirable to enhance the activity and selectivity of the hydrogenation of unsaturated hydrocarbons. However, if elevated temperatures are required for reactions, the subsurface Ni atoms start to diffuse into bulk Pt,leaving a monometallic Pt surface and therefore the disappearance of the enhanced bimetallic hydrogenation activity [17,22] . In addition, as shown in Fig.8, adsorbates such as oxygen can cause the subsurface Ni atoms to segregate to the surface, forming the Ni-Pt-Pt surface that is not active for hydrogenation reactions. One idea to overcome such inherent instability of Pt-Ni-Pt is to replace the bulk Pt with an alternative substrate, such as transition metal carbides that often show catalytic properties similar to Pt [38-44] . We have explored the utilization of tungsten monocarbide (WC) to produce the Pt-Ni-WC structure [45] . As WC has been shown to be an effective diffusion barrier layer [46] , thermal deactivation due to Ni diffusion will be alleviated. Furthermore, it is also possible that the WC substrate would anchor Ni by the formation of W—Ni or C—Ni bonds to prevent its segregation to the surface in an oxygen-rich environment. Fig.10 shows a comparison of the hydrogenation of cyclohexene from Pt-Ni-Pt and Pt-Ni-WC surfaces [45] . The Pi-Ni-WC surface shows higher hydrogenation activity, which is consistent with parallel DFT calculations [45] . The promising results in Fig.10 suggest the possibility to synthesize a more active and stable Pt-Ni-WC hydrogenation catalyst with much lower loading of Pt than that in Pt-Ni-Pt.3.3 Production of hydrogen using bimetallic catalystsAll examples presented above are for hydrogenation reactions, which can be classified as hydrogen-consuming reactions and require catalysts to bond to atomic hydrogen and adsorbates relatively weakly. Using the surface d-band center argument in Fig.3, these reactions are preferred on bimetallic catalysts with surface d-band center away from the Fermi level, such as the Pt-3d-Pt subsurface structures. In contrast, for hydrogen-producing reactions, the desirable catalysts should be those that bond to hydrogen and adsorbates more strongly, i.e., with d-band center closer to the Fermi level, such as the 3d-Pt-Pt surface structures. This hypothesis has been confirmed experimentally in our recent studies for the production of H 2 from the reforming of biomass derived molecules, including ethanol, ethylene glycol and glycerol on the Ni-Pt-Pt(111) surface [47] . Similarly, the Ni-Pt-Pt(111) surface also shows a very high activity for H 2 production from the decomposition of ammonia [48] .We have also demonstrated that coking of the catalyst surfaces, a common deactivation mechanism in dehydrogenation reactions, can be reduced by the formation of bimetallic surfaces [49] . These results further demonstrate the possibility of designing bimetallic catalysts from combined theoretical predictions and experimental verification.4 ConclusionsThe field of catalysis is undergoing a revolution in the selection process of catalytic materials, from the traditional“trial-And-error”method to the“rational design”approach, with the latter requiring atomic level understanding of the catalyst structures and reaction mechanisms. In the current review we utilized several hydrogenation reactions to demonstrate the importance of combining theoretical and experimental approaches for designing bimetallic structures with desirable catalytic properties. In addition, the examples also illustrated the possibility to bridge the “materials gap”and “pressure gap”between fundamental studies on single crystal surfaces and catalytic evaluation of supported catalysts. Similar approaches can be adopted for the rational design of bimetallic catalysts beyond hydrogenation reactions.多相催化领域，特别是在催化作用双金属合金，在过去的几十年里看到了许多进展。
理论与计算催化
SiO2/Mo(110)
0.0
2200
2100
2000
1900
Wavenumber (cm )
-1
1800
0
1
Cu (ML)
2
3
Y. X. Yao, X. F. Ma, W. Goodman, W. X. Li, in preparation
RhCu合金：乙烯氢甲酰化
1.5
(a) 1.37
(b)
CO insertion Hydrogenation
理论与计算催化
结构、组分 电子结构
催化功能 活性、选择性
理解
优化
预言
+
实验合作研究 实用催化剂
Theory of heterogeneous catalysis
• Detailed treatment of specific reactions
– Insight into the quality of theoretical methods (DFT) – Detailed comparison to experiments – Specific examples of the principles behind
理论与计算催化
Literal quote from Kohn and Sham’s paper:“…
Walter Kohn, Nobel Prize 1998 Chemistry
We do not expect an accurate description of chemical binding.”
甲酰基:碳链增长/含氧化物的重要中间体
RHCO RHC O
O/Rh键～235 kJ O/Co键～291 kJ
氢能制储运英语
氢能制储运英语Hydrogen Energy Production, Storage, and Transportation Hydrogen, as a clean and abundant energy source, has gained increasing attention in recent years. In order to utilize hydrogen energy effectively, it is necessary to establish a complete system for hydrogen production, storage, and transportation. In this article, we will discuss the current technologies and challenges in hydrogen energy production, storage, and transportation.Hydrogen Energy ProductionThere are several methods for producing hydrogen, including steam methane reforming, electrolysis, and biomass gasification. Steam methane reforming is the most common method for industrial hydrogen production, but it relies on fossil fuels and produces carbon emissions. Electrolysis, on the other hand, uses electricity to split water into hydrogen and oxygen, and can be powered by renewable energy sources. Biomass gasification can also be used to produce hydrogen from organic materials. While these methods have their advantages and disadvantages, thekey challenge for hydrogen production is to make it cost-effective and sustainable.Hydrogen StorageHydrogen has a low energy density by volume, which makes it challenging to store and transport. There are several methods for storing hydrogen, including compressed gas storage, liquid hydrogen storage, and solid-state storage. Compressed gas storage involves storing hydrogen at high pressures, which requires heavy and expensive tanks. Liquid hydrogen storage requires cryogenic temperatures, which also adds to the complexity and cost of storage. Solid-state storage, such as metal hydrides and carbon nanomaterials, shows promise for safe and efficient hydrogen storage. However, all of these methods have their own technical and economic challenges that need to be addressed.Hydrogen TransportationOnce hydrogen is produced and stored, it needs to be transported to end users such as fueling stations or industrial facilities. Hydrogen transportation can be achieved through pipelines, trucks, or ships. Pipelines arethe most common method for large-scale hydrogen transportation, but they require significant infrastructure investment. Trucks and ships are used for smaller-scale transportation, but they also face challenges such as safety and efficiency. In addition, the development of a global hydrogen transportation infrastructure is still in its early stages.Challenges and Future OutlookWhile hydrogen energy production, storage, and transportation technologies have made significant progress, there are still many challenges that need to be overcome. These include reducing the cost of hydrogen production, improving the efficiency and safety of hydrogen storage, and developing a comprehensive and cost-effective hydrogen transportation infrastructure. In addition, the integration of hydrogen energy into existing energy systems and the development of regulations and standards are also important for the widespread adoption of hydrogen energy.Looking to the future, there is great potential for hydrogen to play a key role in the transition to a sustainable and low-carbon energy system. With continuedresearch and development, as well as collaboration between governments, industries, and academia, hydrogen energy can become a viable and competitive energy source. However, it will require concerted efforts and investments to addressthe technical, economic, and regulatory challenges associated with hydrogen energy production, storage, and transportation.氢能制储运氢作为一种清洁且丰富的能源，近年来受到越来越多的关注。
光催化析氢协同生产高附加值产品文献英文
光催化析氢协同生产高附加值产品文献英文In recent years, the combination of photocatalysis and hydrogenolysis has been widely used in the production of high-value-added products. Photocatalysis is a process in which light energy is used to activate a catalyst to promote the reaction of a substrate. Hydrogenolysis is a process in which hydrogen is used to cleave a substrate into two or more products. The combination of these two processes can be used to produce high-value-added products. The combination of photocatalysis and hydrogenolysis has been used to produce a variety of high-value-added products, such as pharmaceuticals, fragrances, and flavors. Photocatalysis can be used to activate a catalyst to promote the reaction of a substrate, while hydrogenolysis can be used to cleave the substrate into two or more products. This combination of processes can be used to produce high-value-added products with high efficiency and selectivity.In addition, the combination of photocatalysis and hydrogenolysis can be used to produce high-value-added products with low environmental impact. Photocatalysis is a clean and efficient process that does not produce any hazardous by-products. Hydrogenolysis is also a clean process that does not produce any hazardous by-products. The combination of these two processes can be used to produce high-value-added products with low environmental impact.The combination of photocatalysis and hydrogenolysis has been widely used in the production of high-value-added products. This combination of processes can be used to produce high-value-added products with high efficiency and selectivity, and with low environmental impact. This makes it an attractive option for the production of high-value-added products.。
(完整word版)《化学工程与工艺专业英语》课文翻译 完整版
Unit 1 Chemical Industry化学工业1。
Origins of the Chemical IndustryAlthough the use of chemicals dates back to the ancient civilizations， the evolution of what we know as the modern chemical industry started much more recently。
It may be considered to have begun during the Industrial Revolution， about 1800, and developed to provide chemicals roe use by other industries. Examples are alkali for soapmaking， bleaching powder for cotton， and silica and sodium carbonate for glassmaking。
It will be noted that these are all inorganic chemicals。
The organic chemicals industry started in the 1860s with the exploitation of William Henry Perkin’s discovery if the first synthetic dyestuff—mauve. At the start of the twentieth century the emphasis on research on the applied aspects of chemistry in Germany had paid off handsomely， and by 1914 had resulted in the German chemical industry having 75% of the world market in chemicals。
电催化产氢反应机理和催化性能研究
电催化产氢反应机理和催化性能研究随着全球对清洁能源需求日益增长，制氢技术也得到了广泛关注。
传统的制氢方法主要包括热解法和蒸汽重整法，但这些方法通常需要高温高压条件下进行反应，能耗较高，且产物中含有大量的二氧化碳等有害物质。
相比之下，电催化产氢技术具有低温低压、高效率、不产生有害物质等优点，正逐渐成为当前制氢技术研究的热点。
电催化产氢反应的基本原理是利用电流作用下催化剂表面上的原子吸附氢离子、水分子、电子等并进行氢气生成的过程。
电催化产氢主要依赖于催化剂的催化活性和稳定性，因此对电催化产氢反应机理和催化性能的研究具有重要的科学意义和应用价值。
一、电催化产氢反应机理电催化产氢反应的机理和催化剂的选择直接影响反应效率和产物的质量。
近年来，研究者们通过理论和实验手段阐明了电催化产氢的机理，主要包括水分子裂解机理、膜电位、原子加氢和析氢反应等几个方面。
1、水分子裂解机理水分子裂解是电催化产氢反应的关键步骤之一。
传统的水分子裂解机理主要分为两类，即电子传递机理和质子传递机理。
在电子传递机理中，电子从金属表面被传递到水分子中，打破氢氧键，产生氢离子和氧离子；在质子传递机理中，则是通过催化剂表面上的质子通道促进水分子裂解。
2、膜电位在水分子裂解后，产生的氢离子要通过膜电位转化成氢气。
膜电位即膜上一侧的电位和膜另一侧的电位之差。
过高或者过低的膜电位都会影响电催化产氢反应速率和转化率，因此对膜电位的控制和优化也是电催化产氢反应机理研究的重要方向之一。
3、原子加氢和析氢反应电催化产氢反应的最终产物是氢气，其产生过程可以分为三步：原子吸附、原子加氢和析氢反应。
原子吸附是指催化剂表面上的原子吸附氢分子和氢离子；原子加氢是指原子与前面吸附的氢离子或氢分子反应，形成氢原子和水分子；析氢反应则是指另一个原子加氢后，从催化剂表面上解离，生成氢气和催化剂表面的原子。
二、催化性能研究除了机理研究外，实际应用中的电催化产氢反应的催化剂数值设计和优化也十分重要。
低温高压氢制备及储运系统关键技术研究
低温高压氢制备及储运系统关键技术研究下载提示：该文档是本店铺精心编制而成的，希望大家下载后，能够帮助大家解决实际问题。
文档下载后可定制修改，请根据实际需要进行调整和使用，谢谢！本店铺为大家提供各种类型的实用资料，如教育随笔、日记赏析、句子摘抄、古诗大全、经典美文、话题作文、工作总结、词语解析、文案摘录、其他资料等等，想了解不同资料格式和写法，敬请关注！Download tips: This document is carefully compiled by this editor. I hope that after you download it, it can help you solve practical problems. The document can be customized and modified after downloading, please adjust and use it according to actual needs, thank you! In addition, this shop provides you with various types of practical materials, such as educational essays, diary appreciation, sentence excerpts, ancient poems, classic articles, topic composition, work summary, word parsing, copy excerpts, other materials and so on, want to know different data formats and writing methods, please pay attention!随着清洁能源的需求不断增加，氢能作为一种高效清洁能源备受瞩目。
加氢技术考试(试卷编号2251)
加氢技术考试(试卷编号2251)1.[单选题]高压分离器酸性水阀门堵塞的主要物质通常为()。
A)硫化亚铁B)催化剂粉尘C)环烷酸铁答案:B解析:2.[单选题]加氢裂化的反应机理是催化裂化反应叠加加氢反应,其反应遵循的原则是()反应。
A)脱氢B)断链C)正碳离子答案:C解析:3.[单选题]柴油95%馏出温度太高是由于A)反应深度增大B)塔底温度升高C)塔顶回流量增大答案:B解析:4.[单选题]机器工作条件不同润滑油的品种也不同,在高速轻负荷条件下工作的摩擦零件,润滑油应选择()。
A)凝点低B)粘度大C)粘度小答案:C解析:5.[单选题]《危险化学品建设项目安全监督管理办法》规定,对安全审查未通过的建设项目,建设单位( )后可以重新申请建设项目安全条件审查。
A)一个月B)两个月C)经过整改答案:C解析:B)降低压力C)提高压力答案:C解析:7.[单选题]装置操作人员在汽包药剂加注时不慎眼睛里被药水溅入,其应急措施正确的是()。
A)点眼药膏B)马上到医院看急诊C)立即开大眼睑,用清水冲洗眼睛答案:C解析:8.[单选题]关于加氢催化剂作用机理描述,正确的是()。
A)能够改变反应速率B)不能改变反应的活化能C)能够改变化学平衡答案:A解析:9.[单选题]保护听力而言,对听力不会损失,一般认为每天8小时长期工作在()分贝以下。
A)100B)90C)80答案:C解析:10.[单选题]往复式压缩机排出压力下降,排除工艺系统和仪表故障外,还可能是( )故障。
A)机械B)仪表C)电气答案:A解析:11.[单选题]加氢装置开工阶段氢气引入系统时要求反应器床层最高温度不超过()℃。
A)230B)250C)150答案:C解析:A)新投用的催化剂活性较高导致反应转化率较大B)此事故是分馏系统冲塔,跟反应岗位操作人员无关C)在开工中切换VGO时,装置人员没有查看原料油分析数据,没有注意各指标确认答案:B解析:13.[单选题]循环氢脱硫塔差呀上升导致循环氢压缩机入扣缓冲罐高液位联锁停机,循环氢脱硫塔压差高的应对措施不正确的是()。
加氢催化剂技术协议书
加氢催化剂技术协议书本协议旨在明确加氢催化剂技术的相关要求和合作细节，确保双方权益得到保障。
以下是协议的主要内容：一、协议双方甲方：（以下简称“甲方”）乙方：（以下简称“乙方”）二、技术要求和标准1. 乙方应按照甲方的要求，提供符合国家标准和行业标准的加氢催化剂产品。
2. 乙方应确保所提供的加氢催化剂产品具有优异的催化性能、稳定性和可靠性，能够满足甲方生产需求。
3. 乙方应提供加氢催化剂产品的详细技术资料，包括产品说明书、技术规格书、工艺流程图等。
三、合作方式和期限1. 双方同意采取长期合作的方式，共同推进加氢催化剂技术的研发和应用。
2. 合作期限自本协议签订之日起，至双方协商确定的终止日期止。
四、价格和支付方式1. 双方应根据市场情况和产品成本，协商确定加氢催化剂产品的价格。
2. 甲方应按照约定的时间和方式支付货款，确保乙方能够及时获得收益。
五、保密条款1. 双方应对涉及加氢催化剂技术的商业秘密和保密信息予以严格保密，未经对方同意，不得向任何第三方泄露。
2. 双方应采取合理的技术和管理措施，确保保密信息不被泄露、滥用、丢失或损毁。
六、违约责任1. 如乙方未能按照约定提供符合要求的加氢催化剂产品，应承担相应的违约责任，并赔偿甲方因此造成的损失。
2. 如甲方未能按照约定支付货款，乙方有权要求甲方支付违约金或采取其他合法手段维护自身权益。
七、争议解决方式如双方在执行本协议过程中发生争议，应首先通过友好协商解决；协商不成的，可以向有管辖权的人民法院提起诉讼。
八、其他条款1. 本协议一式两份，甲乙双方各执一份。
本协议自双方签字（或盖章）之日起生效。
2. 本协议未尽事宜，双方可另行协商补充。
经双方协商一致，可以签订补充协议，补充协议与本协议具有同等法律效力。
3. 本协议的解释权归甲乙双方共同拥有。
甲方：（签字/盖章）日期：乙方：（签字/盖章）日期：。
外文翻译--动力学研究与二氧化硫反应在低温和氢氧化钙在一固定床反应器
翻译部分英文原文Kinetic study of the reaction between sulfur dioxideand calcium hydroxide at low temperature in afixed-bed reactorAbstractA quantitative study of the influence of inlet sulfurdioxide concentration (600–3000 ppm),relative humidity (20–60%), reactortemperature(56–86℃)and different amounts (0–30 wt.%) ofinorganic additives(NaCl, CaCl2 andNaOH) on gas desulfurization has been carried out in acontinuous downflow fixed-bed reactor containing calcium hydroxide diluted with silica sand.Results show that the reaction rate does not depend on sulfur dioxide partial pressure (zero-order Kinetics) and that the temperature and the relative humidity have a positive influence on reactionrate. An apparent activation energy of 32 kJ/mol Ca(OH)2 has been estimated for the reaction.An empirical reaction rate equation at 71.5℃and 36.7% relative humidity that includes thetype and amount of additive is proposed. It has been found thatcalcium chloride is the bestadditive studied because it allows for a higher degree of sulfur dioxide removal. 2000 ElsevierScience B.V. All rights reserved.Keywords: Desulfurization; Sulfur dioxide; Calcium hydroxide; Kinetics; Inorganic additives1. IntroductionThe increasing concern during the last few years on the protection of the environmenthas had its influence on the design and operation of power plants, especially on thereduction of sulfur dioxide and nitrogen oxide emissions from them. They are the mainpollutants from coal and fuel-oil combustion in power plants. Both gases are responsiblefor acid rain.In USA and Europe, new power plants that use fuels with significant quantities ofsulfur have to meet severe standards to reduce these air pollutants. One of the majorproblems facing older power plants is that they were designed prior to the presentstandards for pollution control and therefore have no facilities on space to incorporatesuch controls.The technologies to control sulfur dioxide emissions can be distributed into threegroups by considering if the treatment is done before, during or after thecombustion. Itseems clear that the last group of technologies cited is the most advantageous, fromvarious points of view, for power stations which have been in operation for many years.These are called FGD technologies (Flue Gas Desulfurization),and among them, themost usedare: IDS (In-Duct Scrubbing, developed by General Electric); E-So x(developed by US EPA, Babcok and Wilcox, Ohio Coal Development Office and OhioEdison), EPRIHYPAS (Hybrid Pollution Abatement System, developed by ElectricPower Research Institute), DRAVO HALT (Hydrate Addition at Low Temperature,developed by Dravo), CONSOL COOLSIDE (developed by Consolidated CoalCom-pany)and ADVACATE(developed by Acurex and US EPA). These processes are basedon the injection of a solid sorbent plus water by spraying or injecting a slurry into theduct situated between the air preheater and the particulate collection system. Calciumhydroxide or limestone are usually used as sorbents to capture sulfur dioxide and acalcium sulfiter/sulfate mixture is obtained as the reaction product.Klingspor and Stromberg proposed a mechanism to explain the reactionbetween sulfur dioxide and calcium hydroxide or calcium carbonate in the presence ofwater vapor. According to them, when the relative humidity is low (below 20%), sulfurdioxide and water can be adsorbed on the solid surface, however, no reaction occursuntil there is at least a monolayer of water molecules adsorbed on the surface. As therelative humidity increases, less sulfur dioxide can be adsorbed on the surface becausewater adsorption on the solid occurs preferentially due to intermolecular forces. Thus,sulfur dioxide has to be absorbed on the adsorbed water, forming complexes where thesulfur atom isbound to the oxygen atom of water. This fact leads to the formation of apositive charged hydrogen atom that can combine with hydroxide or carbonate ions fromthe sorbent to form reaction intermediates and products. Experimental findings show thatthe reaction rates for lime and limestone are similar. Consequently, the complexformation SO2nH O is considered to be the rate-determining step, since all further reactions are different for the two types of sorbents. The initial rate of the process isindependent of sulfur dioxide concentration when the relative humidity is below 70%.Above this value, the reaction rate becomes gradually more and more dependent on thesulfur dioxide partial pressure. This fact can be attributed to the formation of stableconfigurations of water ligands around the sulfur dioxide molecules. Also, it has beenfound that the initial reaction rate is a very weak function of temperature but increasesexponentially with relative humidity, for both hydrated lime and limestone.Jorgensen also studied this reaction in a bench-scale sand bed reactor. Someof their conclusions point out that the calcium hydroxide conversion has a very strongdependence on relative humidity. The conversion rate is increased moderately withtemperature in agreement with activation energy of 25 kJ/mol. However, there is noclear indication of increasing conversion with increasing sulfur dioxide concentration.Ruiz-Alsop and Rochelle found that the relative humidity is the most importantvariable affecting the reaction of sulfur dioxide and calcium hydroxide. The chemicalreaction taking place at the surface of the unreacted calciumhydroxide presentszero-order kinetics in sulfur dioxide. At high relative humidity and/or high SO2concentration, the chemical reaction at the surface of the unreacted calcium hydroxidesolid controls the overall reaction rate. At low relative humidity and/or low sulfurdioxide levels, diffusion of sulfur dioxide through the solid product layer becomes therate-controlling step. The reaction rate has a weak temperature dependence. Theactivation energy of the reaction was estimated to be 12 kJ/mol.Experimental data by Krammer showed that the reaction ratedepends onthe sulfur dioxide concentration but only at low concentrations and not so obvious athigher concentrations. In contrast to other publications, they found that the influence ofSO2concentration on the reaction rate is rather linked to the conversion than to the 2relative humidity, which has a major impact on the conversion throughout the entirereaction as usually reported in literature. But they found out that the initial reaction rateseems to be independent of relative humidity and sulfur dioxide concentration, whichhad not been reported yet. They postulated that the reaction can be divided into thefollowing foursteps. During the initial stage, a chemisorption process of the sulfurdioxide on the particle surface seems to be important and the reaction rate decreasesexponentially with increasing conversion. Simultaneously, a nucleation processdominates the formation of the consecutive product layers where the reaction rateincreases with increasing relative humidity. The rate of reaction increases untilproduct layer diffusion takes over and reaction rate decreases again with conversion. Itshould be noted that only relative humidityhas an impact on product layer diffusion. Beyond a conversion of around 9%, reaction rate drops significantly, which can be dueto pore closure.Irabien consider the adsorption of sulfur dioxide on calcium hydroxideacting as a nonideal solid sorbent is the rate-limiting step. They use a parameterreferring to this nonideal behavior of the solid surface as independent of temperature butexponentially dependent on relative humidity. The authors obtained activationenergy of75 kJ/mol for the reaction.All published work thus far indicates that relative humidity has the greatest impact onthe reaction rate between sulfur dioxide and calcium hydroxide. The relative humidity isin turn correlated with the moisture content of the solids. Additives that will modify themoisture content of the calcium hydroxide solids in equilibrium with a gas phase of agiven relative humidity would then be expected to enhance the reactivity of calciumhydroxide towards sulfur dioxide in FGD processes.Organic and inorganic additives have been tested in spray dryer systems to improvethe desulfurization power of calcium hydroxide and calciumcarbonatew.It seems that inorganic hygroscopic salts such as barium, potassium, sodium and calciumchlorides and also cobalt, sodium and calcium nitrates would be the most effective ones.Some researchers also consider sodiumhydroxide as an effective additive due to itsalkaline and hygroscopic properties.Ruiz-Alsop and Rochelleindicated that deliquescence alone does notexplainthepositive effect of some salts. They contend that for an additive to be effective, it is alsonecessary that the hydroxide of the cation be very soluble, otherwise, the cation willprecipitate out as the hydroxide and the anion will form the calcium salt which could notbe hygroscopic. The effectiveness of a certain salt also depends on the relative humidity.This could be expected because when therelative humidity of the gaseous phase islower than the water activity in a saturated solution of the salt, it would not absorb waterand so, it would not enhance the calcium hydroxide reactivity. These researcherscontend that chlorides and sodium nitrate modify the properties of the product (half-hy-drated calcium sulfite) layer that is formed as the reaction takes place, therebyfacilitating the access of sulfur dioxide to unreacted calcium hydroxide, which remainsin the interior of the particle.The scope of the present work is to quantify the influence on the reaction rate ofsulfur dioxide concentration, relative humidity, temperature and type and amount ofadditive. An empirical equation, which relates the reaction rate with these variables, hasbeen obtained and an apparent activation energy value for the reaction has also beendetermined from kinetic constants at different temperatures by using the Arrhenius plot.2. Experimental sectionThis equipmentconsists of a continuous feeding and humidification system of a gaseous stream, afixed-bed reactor and an analytical system. The apparatus is operated with a personalcomputer using LabView software (NationalInstruments), which allows programmingand control of the experimental conditions, namely, nitrogen and sulfur dioxide flowrates, humidification temperature and electric resistance heating of the pipes to avoidcondensations and also provides the experimental data acquisition, in particular nitrogenand sulfur dioxide flow rates, reaction temperature, pressure, relative humidity andsulfur dioxide concentration, vs. reaction time.Simulated flue gas was obtained by mixing sulfur dioxide and nitrogen from separatecylinders in appropriate amounts using mass flow controllers Before mixing, pure nitrogenwas passed (by switching on valve 1 from thecomputer)through the humidificationsystemthat consisted of three cylindrical flasks with 200 ml of watereach submerged into a thermostatic bath. Each flask contains small glass spheres toimprove the contact between gas and water. After the humidification system, thetemperature and the relative humidity of the wet nitrogen were measured by using aVaisala HMP 235 transmitter .At the same location, the pressure was alsoMeasuredto calculate the flow rate of water vapour generated. Thewet nitrogen by-passed the reactor until the desired experimental conditionswerereached and then valve 2 was opened from the computer to allow thegaseous streamflow through the reactor. The bed was always humidified for 15 min while the sulfurdioxide analyser was set to zero. At this time, the desired flow of sulfur dioxide wasintroduced by a mass flow controller and the experiment began. Data generated duringthe experiment were stored in an EXCEL format computer file.The glass reactor, a jacketed Pyrex tube (450 mm height, 12 mm i.d.)with a porousplate to hold 1 g of dry calcium hydroxide (Probus, 99% purity and particle size smallerthan 0.05 mm in diameter)or calcium hydroxide–additive mixtures(all additives weresupplied by Fluka, 99% purity and particle size smaller than 0.05 mm in diameter) diluted with 8 g of silica sand (Merck;0.1–0.3 mm in diameter)to assure isothermaloperation and to prevent channelling due to excessive pressure drop, was thermostatedby pumping a thermal fluid (water–ethyleneglycol mixture) from an external thermostaticbath.The reacted flue gas is passed through a refrigeration systemin orderto remove water because it interferes with the SO2 analyser measurement.The output from the analyser was continu-ously collected by the computer for 1h (experiment time)and the concentration (ppm) of sulfur dioxide stored as a function of time (experimental curve). Each experiment wasconducted in the same manner except a reactive solid was substituted for the10 g ofinert silica(‘‘blank’’ experiment) to obtain a reference flow curve. The reaction rate wascalculated as SO2mol removed/h mol OH-from the area enclosed by the two curves (experimental and ‘‘blank’’). Some experiments were replicated to estimate the experimentalerror in reaction rate.3. ConclusionsIn this research, the quantitative influence of sulfur dioxide concentration, temperature,relative humidity and the type and amount of the three inorganic additives on thereaction rate between calcium hydroxide and sulfur dioxide have been determined.The SO2concentration (0–3000 ppm)was shown to have no significantinfluence on the reaction rate at a relative humidity of 38% and at 71.5℃. These results agree withthose of Ruiz-Alsop and Rochelle who indicated that sulfur dioxide concentrationdoes not influence the reaction rate at temperatures ranging from 30℃to 90℃; 17–90%relative humidity and sulfur dioxide concentration varying from 0 to 4000 ppm. Sinceour experiments are within the range of these experimental conditions, we assume thatsulfur dioxide concentration will not influence the reaction rate at our other experimentalconditions also.An empirical rate equation, which allows us to quantify the influence of temperatureand relative humidity on reaction rate has been developed and an apparent activationenergy of 32 kJ/mol Ca(OH)2 has been calculated. This value, relatively high, demonstrates the weak influence of temperature, but the reaction order of 1.2 withrespect to the relative humidity shows its strong influence on reaction rate.Three inorganic additives were tested to evaluate their quantitative influence onreaction rate. An empirical equation for each additive at 71.5℃and a relative humidityof 36.7% was developed.The kinetic rate constants for calcium chloride, sodium hydroxide and sodiumchloride were found to be respectively, 9, 5 and 0.81 times the rate constant for calciumhydroxide without any additive. The reaction orders for the weight ratio of the sameadditives were 0.6, 0.52 and y0.12, respectively. Calcium chloride is the best additivewhereas sodium chloride is an inhibitor.中文译文动力学研究与二氧化硫反应在低温和氢氧化钙在一固定床反应器摘要一个入口二氧化硫浓度（600-3000百万分之一），相对湿度（20-60％），反应器温度（影响的定量研究56-86℃）和不同的金额（0-30%重量）ofinorganic添加剂（氯化钠，氯化钙和氢氧化钠）对气体脱硫已进行acontinuous下行流了固定床反应器含有氢氧化钙与氧化硅sand.Results 稀释表明，反应速度不依赖于二氧化硫分压（零阶动力学），而温度和相对湿度对reactionrate积极的影响。
化工毕业实习报告
化工毕业实习报告篇一：化工毕业实习报告毕业实习报告系别：专业：姓名：学号：指导教师：完成时间：河南城建学院XX年 03 月 13 日前言一实习目的1毕业实习和毕业设计是化工专业学生进行专业训练的必要环节，是毕业生综合运用大学所学专业知识，理论联系实际，进行融会贯通的独立思考，锻炼和提高学生综合运用理论知识和技能的能力，独立工作和创新能力。
学生在进行毕业设计之前，通过毕业实习的教学环节，学生有针对性的以比较长的时间参与化工生产过程及化工单元操作，使学生对设计（论文）方向的化工生产单元操作的理论计算的理解和掌握更加深刻和熟练，为毕业设计（论文）奠定坚实的基础。
任务：根据毕业设计（论文）课题，有选择的参与实习工厂化工生产过程中的某些单元操作，了解和熟悉这些单元操作生产过程操作、工艺参数、设备结构及工作原理。
查阅相关设计资料，初步了解设计方法及步骤。
2 (1) 注意安全。
实习期间不允许单独行动，严格遵守实习单位的安全条例和各项规章制度，遇到突发事件要及时向带队老师报告。
实习期间要作到一切行动听指挥，尊重工人师傅，虚心向工人师傅请教。
(2) 不迟到，不早退，有事须向老师请假,敢于创新，勤于实践，爱护仪器设备，严格遵守操作规程和各项规章制度。
(3) 学生在掌握化工理论和确定设计（论文）题目的基础上，深入生产一线直接参与设计（论文）相关的化工生产过程，进一步掌握与设计（论文）内容相关化工生产的规律，熟悉其流程、参数、设备及生产过程及配套设施。
(4) 了解设计过程，查阅设计文件（图纸）并收集有关数据、资料。
二实习基本内容（1）合成氨、合成尿素等化工生产过程：要求理解和掌握焦炉煤气净化、制氢、合成氨、合成尿素等生产过程的开、停车、正常操作、事故处理等操作步骤。
（2）化工生产控制：要求了掌握该生产过程中，重要的监测和控制生产过程的仪表的工作，了解其工作原理，理解化工仪表及自动化在化工生产过程中的作用。
（3）化工生产工艺及设备：要求进一步掌握焦炉煤气净化、制氢、合成氨、合成尿素等化工生产装置工艺流程、主要设备的结构、原理及主要工艺操作参数。
加氢催化剂技术协议书
加氢催化剂技术协议书
夫协议书者，乃双方意志之合，共守之规也。
今有吾等与贵方，就加氢催化剂技术之事，议定如下：
一、技术之范围
本协议所涉及之技术，乃加氢催化剂之制备、应用及其相关之工艺也。
具体包括但不限于催化剂之成分、结构、性能及其在生产过程中之优化措施等。
二、技术之交流
双方应定期或不定期举行技术交流会，以共同探讨催化剂技术之发展及应用。
吾等当以所知所学，倾囊相授，贵方亦应坦诚相待，共谋进步。
三、技术之保密
双方在此协议中所获得之对方技术资料及商业秘密，均应严格保密，未经对方书面同意，不得向任何第三方泄露或用于其他非协议约定之用途。
四、技术之应用与改进
贵方在应用本协议所提供之技术时，应遵守相关法律法规及行业标准，确保安全生产及环境保护。
同时，双方应共同努力，不断改进催化剂技术，以提高其性能及降低成本。
五、违约责任
若任何一方违反本协议之约定，均应承担相应之违约责任。
具体责任及赔偿方式，由双方协商确定。
六、协议之变更与终止
本协议在执行过程中，若遇有不可抗力或其他特殊情况需要变更或终止时，应由双方协商一致，并以书面形式确认。
以上所述，皆为本协议之要义。
双方共同遵守，以期共赢。
谨以此书，为凭。
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的合成 与表征， 负载型催化剂 的制备号 ｌ能测试等． 生 其次， 总结了双金属催化剂在其他加氢反应， 如丙烯醛 Ｃ ＝Ｏ 双键的选择性加氢， 的低温加氢， 苯 以及 乙炔 的选择性加氢等反应 中的应用． 最后 ， 讨论 了利用金属碳化物代替
贵金属 Ｐ 以减少双金属催化剂 中 Ｐ 用量 的可能性 ． ｃ ｔ
物理化 学学报 （ ｌＨｕｘｅ ｕｂ ｏ Ｗｕｉ ａｕ ｅａ ） Ｘ
Ａｐｒｌ ｉ
ＡｃａＰｈ ｓ － ． ｉ．２ １ ， ６ ４ ： ６ — ７ ｔ ｙ ． Ｃ Ｓｎ， ０ ０ ２ （）８ ９ ８ ６
［ ｖｅ Ｒｅ ｉｗ】
ｗｗｗ． ｘ ｐ ．ｄ ｃ ｗｈ ｂ．ｋｕｅ ｕ．ｎ
Ｃ Ｅ ｎ ｇ ａ ｇ Ｈ ＮＪ ｇ ｕ ｎ ’ ｉ Ｇ Ｑ ｕ— ａ Ｉ ｉ ｏ Ｓ Ｔ 。 Ｈ ＵＭＢ Ｒ ｃ ａｌ Ｅ ＴＭｉ ｅ Ｐ ｈ Ⅳ 正Ｎ Ｎ ａｌ ＮＩ Ｇ Ｃ ｒ Ａ Ｚ Ｕ Ｙ ｅＸ ａｇ Ｈ ｕ — ｉｎ 。
（ ｅａｔ ｅｔｆ ｈｍｉ ｌ ｎ ｉｅｒ ｇ Ｃ ｎｅｆ ｒ ａａ ｔ ｃ ｎ ｅ ｎ ｅｈ ｏ ｇ Ｃ Ｔ， ｎｖｒｔ ｏ Ｄ ｌｗ ｒ， ｅ ａ Ｄ ｐ ｒ ｎ Ｃ ｅ ｃ ｇｎ ｅｉ ， ｅ ｔ ｏ ｔｙｉＳ ｉ ｃ ｄＴ ｃｎ ｌ ｙ Ｃ Ｓ ）Ｕ ｉ ｓｙｆ ｅ ａｅ Ｎ ｗ 心 Ｅ Ｄ ｍ ｏ ａＥ ｎ ｒ Ｃ ｌｃ ｅ ａ ｏ ｒ ｅ ｉ ａ
Ｃ ｌｇ ｈｍ ｓ ｄ ｌｃｌｒ ｎ ｉ ｅｉ ， ｅ ｉ ｎｖｒｉ， ｅ ｉ １ ０ ７， ． ． ｈｎ） ｏｌ ｅ Ｃ ｅ ｉ ｒ ａ ｅ ｕ ｇｎ ｒ ｇ Ｐ ｋ ｇＵ ｉ ｓ Ｂ ｉｎ ｅ ｏ ｆ ｔ ｎ Ｍｏ ｙ ａＥ ｅ ｎ ｎ ｅ ｔ ｙ ｊ ｇ ０ ８ １Ｐ Ｒ Ｃ ｉａ
低 温加 氢催 化 剂 的设计 ： 论与 实践 理
陈经广 ， 齐随涛 ， Ｍ Ｎ ＩＧ ａＡ ＥＮＮ Ｃｒ ｌ
Ｄ １ ７ ６ＵＳ Ｅ ９ １， Ａ； 。 西安交通大学化工 系， 西安
Ｈ Ｍ ＥＴ ｉａ Ｕ ＢＲ ｃ ｅ Ｍ ｈｌ Ｐ 朱 月香 。
（ ｅ ａ ｍ ｎ ｆ ｈ ｍｉ ｌ ｎ ｉｅｒ ｇ Ｃ ｎｅ ｆｒ ａ ｌｔ ｃ ｎ ｅ ｎ ｅ ｈ ｏｏ ｙ（ Ｃ Ｔ ， ｎｖ ｒ ｔ ｏ ｅａ ａｅ Ｎ ｗａ ， １ ｐ ｒ ｅ ｔ ｅ ｃ ｇ ｅ ｎ ， ｅ ｔ ｔ ｙ ｃ ｉ ｃ ｄ ｃ ｎ ｌｇ Ｃ Ｓ ） Ｕ ｉｅｓ ｙ ｆ ｌｗ ｒ， ｅ ｒ Ｄ ｔ ｏＣ ａＥ ｎ ｉ ｒｏＣ ａ ｉ Ｓ ｅ ａ Ｔ ｉ Ｄ ｋ
ｂ ｍｅａ ｌ ｕ ｆ ｃ ｓａ ｄ ｃ ｔ ｙ ｔ ｆ ｒ ｅｌ ｗ—ｅ ｅ ａｕ ｅｈ ｄ ｏ ｅ ａ ｏ ｆ ｎ ａｕ ａｅ ＝ Ｃ ｄＣ＝ Ｏ ｏ ｄ ． ｅｗｉ ｉ ｔｌ ｃｓ ｒａ ｅ ａａ ｓ ｏ ｉ ｎ ｌ ｓ ｈ ｔ ｏ ｔ ｍｐ ｒ ｔｒ ｙ ｒ ｇ ｎ ｔ ｎｏ ｓ ｔ ｒ ｔｄ Ｃ ｉ ｕ ｎ ａ ｂ ｎ ｓＷ ｌ ｌ ｆ ｓ ｕ ｅｔ ｅ ｈ ｄ ｏ ｅ ａｉ ｎ ｏ ｙ ｌ ｈ ｘ ｎ ｓａｐ ｏ ｅ ｒ ａ ｔ ｎ ｔ ｅ ｎ ￣ ｔ ｅ ｉ ｏ ｔ ｎ ｅ ｏ ｓｎ ｅ ｅａ ａ ａｌｌ Ⅱ ． ｔ ｓ ｙ ｒ ｇ ｎ ｔ ｆｃ ｃ ｏ ｅ ｅ ｅ ａ ｒ ｂ ｅ ｃ ｏ ｏｄ ｍｏ ｓ ａｅ ｔ ｍｐ ｒａ ｃ ｆｕ ｉ ｇ ｓ ｖ ｒ ｌ ｒ ｌ ｈ ｏ ｉ ｈ ｐ ｅ
关键词 ： 加氢； 双金属催化剂； 金属碳化物 ； ＤＦ 计算 Ｆ
中 图分 类 号 ： ０ ４ Fra bibliotek６３Ｒａ ｉ ｎ ｌ ｔｏ ａ ｓ ｇ ｆＬｏ Ｔｅ ｐ ｒ ｔ ｒ ｄ ０ ｅ ａ ｉ ｎ Ｃａ ａ ｙ ｔ ： Ｄｅ ｉ ｎ ｏ ｗ－ ｍ ｅ ａ ｕ ｅ Ｈｙ ｒ ｇ ｎ ｔ０ ｔ ｌ ｓ ｓ Ｔｈ ｏ ｅ ｉ ａ ｅ ｉ ｔｏ ｓａ ｐｅ ｉ ｅ ｔ ｌ ｅ ｒ ｔｃ ｌＰｒ ｄ ｃ ｉ ｎ ｎｄ Ｅｘ ｒｍ ｎ ａ ｒｆｃ ｔｏ Ｖｅ ｉｉ ａ ｉ ｎ
７ ０４ ； 。 １０ ９ 北京大学化学与分子工程学院， 北京分子科学国家实验室，
分子动态与稳态结构 国家重点实验室， 北京 １０ ７ ） ０８１ 摘要 ： 简要总结 了我们在 Ｃ Ｃ及 Ｃ ＝ ＝Ｏ双键低温加氢双金属催化剂方面的最新研究成果． 首先， 我们 以环 己 烯加氢为探针反应， 证明了平行使用多种研究手段的重要性， 括单 晶表面的基础研究与 Ｄ Ｉ计算 ， 晶表面 包 Ｆ＂ 多
１ ７ ６ Ｕ Ａ ２ｅａｔ ｅｔ Ｃ ｅ ｃｌ ｎ ｉｅｒ ｇＸ ｎ ｉ ｔ ｇＵ ｉ ｒ ｔ Ｘ ｎ ７０ ４ ， ． ． ｈ ａ ３ｅ ｉ ａｉ ａ ９ １ ， Ｓ ； Ｄ ｐ ｒ ｎ ｈｍｉ ｇ ｅｉ ， ｉ ａ ｏ ｎｖ ｓ ， ｉ １ ０ ９Ｐ Ｒ Ｃ ｉ ； Ｂ ｉｎ Ｎ ｔ ｎ ｌ ｍ ｏ ｆ ａＥ ｎ ｎ ａＪｏｎ ｅｉ ｙ ａ ｎ ｊｇ ｏ Ｌ ｂｒｔｒｆｒ ｌ ｕ ｒ ｃ ｎ ｅ， ｔｔＫ ｙＬ ｂ ｒｔｒｆ ｒ ｔ ｃ ｒｌ ｈｍｉｒ ｎｔｂｅ ｎ ｔｂｅ ｐ ｃ ｓ ａ ｏａｏｙ ｏ ｅ ｌ ｉ ｃｓＳａｅ ｅ ｏａｏ ｏ ｒ ｔ ａ ｅ ｓ ｏ Ｕ ｓ ｌａ ｄ ａ ｌ Ｓｅｉ ， Ｍｏ ｃ ａ Ｓ ｅ ａ ｙ Ｓ ｕｕ Ｃ ｔ ｆ ｙ ａ Ｓ ｅ