新型辊压机DAC弧形双曲线进料装置的特性分析

针对辊压机进料装置的运动轨迹对系统效能影响较大，本文设计了一种新型DAC双曲线进料装置，对其结构组成进行了分解。通过对进料口、侧挡板、调节插板和驱动装置等四个关键要素的研究，提出了沟谷聚落式进料口、同轴层叠式侧挡板、透空式斜插板及智能一体化执行器的设计方法，并将结构特性进行了分析。经过产品设计后应用的情况，结果表明该DAC弧形双曲线进料装置可以将联合粉磨系统产量由210 t/h提高到237 t/h，提升幅度为12.8%，电耗由34.2 kWh/t降至31.9 kWh/t，增产节能效果比较明显。     

连续重整进料换热器压降高原因及对策

重整进料换热器是重整装置重要设备，其性能直接影响到装置的能耗及安全平稳运行。某炼化重整进料缠绕管式换热器在2020年检修后出现进料侧压力降升高的现象，导致重整能耗上升，循环氢压缩机喘振，影响装置的安全平稳运行。本文分析了重整进料换热器进料侧压力降升高的原因和采取的措施，为国内同类装置的运行提供经验。     

VA-90气态原子化装置与AAS联用测定饮用水中汞

介绍了气态原子化装置，以及气态原子化装置与ＡＡＳ联用时，不测定汞元素的精确度、回收率和最低检测限。     

关于改进球磨机进料点的探讨

本文通过利用球磨机粉磨动力学原理，针对实际生产中球磨机粗磨仓的一种不合理现象，对球磨机内抛落式运动时研磨体和物料的运动轨迹及相互之间的作用力进行分析，探求此现象之根源。发现球磨机进料装置在进料点选择上存在不合理之处。通过改进，从而提高球磨机粉磨效率和降低消耗。     

辊压机常见进料装置比较分析

辊压机配套进料装置对联合粉磨系统能效影响较大，通过分析常见的双杠杆、双插板及双曲线进料装置的结构原理和优缺点，结合其使用效果，最终选择双曲线进料装置实现节能降耗的目标。     

用于甲苯歧化与C9芳烃烷基转移过程先进控制的反应动力学模型

针对某实际工业装置，建立了甲苯歧化和C₉芳烃烷基转移反应简化机理模型，用于反应过程的监控、优化及大型轴向流反应器内各物料组成分布的预测；采用四-五阶Runge-Kutta法对模型方程进行了数值求解，并基于多套稳态平衡数据，采用Broyden-Fletcher-Goldfarb-Shanno(BFGS)优化算法对动力学模型参数进行了估计；针对不同的进料组成和操作条件，对工业装置进行模拟仿真。结果表明，模型估计值与工业标定值相当吻合，达到了工业应用的模拟精度要求。所建立的模型形式简单、参数估计方便，适用于工业装置的离线仿真和在线软测量。     

芳烃联合装置深度热集成的节能优化

寻找芳烃装置内部可优化利用的富余热量，重复利用达到节能效果。经研究发现脱庚烷塔顶气相和吸附进料的热量富余较多，废热利用潜力较大。通过增加换热设备，优化换热集成网络，将脱庚烷塔顶气相物料与该塔进料进行换热，将吸附进料物料作为成品塔热源，从而达到降低装置瓦斯消耗，节能降耗的目的。     

用两种不同的流股由乙酸羰基化生产乙醇(续)

<正>(上接第2期第41页)[0041]采用蒸馏系统,该方法提供了回收粗乙酸和回收催化剂溶液,甲基碘,乙酸甲酯和该方法中的其它系统组分的方法。在典型的羰基化方法中,将一氧化碳连续引入羰基化反应器中,理想地在搅拌器下方,用于搅拌内容物。通过该搅拌装置将气态进料彻底分散在反应液体中。希望从反应器中排出气态吹扫气流,以防止气态副产物的积累,并在给定的总反应器压力下保持设定的一氧化碳分压。控制反应器的温度,并以足以维持所需的总反应器压力     

RP170-120辊压机进料装置的改造#br#

我公司共有4台Φ4.2m×14m水泥磨，配套使用的是中信重工RP170-120辊压机，其中1#辊压机在之前已改为双杠杆进料装置，其余3台目前使用的是原设备配套的进料装置。原进料装置最大的弊端就是挤压辊两端漏料严重，影响挤压效果，此前我们频繁调整侧挡板顶丝，改造侧挡板顶丝结构，但效果都不理想。2017年7月，我公司对4#辊压机进料装置进行了改造，成功解决了挤压辊两端漏料的难题。     

正位移式阀控能量回收装置盐水连续进料过程特性研究

能量回收装置是反渗透海水淡化系统的关键设备之一，对降低系统运行能耗和造水成本至关重要。正位移式阀控能量回收装置以反渗透淡化系统排放的高压盐水作为进料，通过在水压缸中直接增压原料海水的方式来实现压力能回收利用。但在装置运行过程中常常存在高压盐水进料不连续（即流量有较大波动）等问题，直接影响了反渗透淡化系统运行的稳定性。本丈在分析造成上述问题原因的基础上，通过改进控制方案，使得高压盐水进料过程中的流量和压力波动问题得到有效解决，保证了盐水进料的连续性。针对阀控能量回收装置运行过程中低压进料海水仍存在流量和压力波动的现象，文章提出了两个具体的措施，即通过多套装置并联运行及在进料海水管路上设置旁路的方式来解决。     

Pyrolysis of the mixture of biomass and plastics in countercurrent flow reactor Part I: Experimental analysis and modeling of kinetics

A shaft kiln is considered to be a promising pyrolysis device for the efficient decomposition of municipal wastes. In this device, the temperature distributions of the gas and solid phases can be separately controlled, thereby leading to considerably different profiles for both the phases. The temperature controllability in a shaft kiln helps us to obtain a suitable profile of the gas-phase temperature for the decomposition of tar that evolves from the solid phase. By leveraging this advantage of the shaft kiln, we performed further pyrolysis and steam reforming of the volatiles formed from the pyrolysis of biomass and several polymers using a two-stage reactor that was maintained at different temperatures. The amount of tar decreased with an increase in the temperature in the upper reactor in the absence of a catalyst. By using the experimental results, we developed a lumped kinetic model for secondary gas-phase reactions and performed a kinetic analysis of the reactions that proceeded in the upper reactor. It is confirmed that the simulation model is successful in reproducing the product distribution of the gas-phase reactions of volatiles from biomass and polymers.     

A PROCESS FOR DISPOSAL OF HALON 1301 (CBrF3)

We report the results of an experimental and kinetic modeling study of gas-phase reaction between methane and halon 1301 (CBrF³). At 1000 K, with an equimolar feed of CH⁴ and CBrF³ and at a residence time of 1 second, CHF³ and CH³Br are produced at selectivities in excess of 90%. Other reaction products detected include C²H²F², C²H², C²H², and CHBrF². Very good agreement between kinetic modeling and experimental results was obtained.     

Kinetics on a Second Scale at Temperatures up to 2300 K—The Reduction of Manganese Oxide in a Solar Furnace

Testing the chemical stability of high-performance ceramics at temperatures above 1800 K is a demanding task. With the aim to provide an experimental set-up for kinetic studies on gas releasing reactions at temperatures up to 2300 K, a solar reactor has been interfaced to a mass spectrometer. Tracer experiments revealed that the reactor behaves as a continuous ideally stirred tank. This characteristic provides a straightforward path to extract kinetic data for such reactions from gas-phase analysis. The approach is demonstrated by presenting results of a study on the solar thermal reduction of manganese oxide at 2200 K.     

PX氧化反应动力学模型研究

建立了一套半连续的PX高温催化氧化反应动力学实验装置,并进行了相关的动力学研究。依据实验数据和机理分析,提出了反应组分抑制的动力学模型。     

生物质快速热解流化床反应器气力进料特性

为探究不同工况下热解流化床反应器的气力进料特性,设计并搭建了流化床反应器气力进料冷态试验装置。生物质原料和床料分别采用落叶松颗粒和石英砂颗粒,通过试验测得了本装置的最小流化速度,研究了流化气速、喷动气速、流量比、初始静床高、石英砂粒径、落叶松粒径对流化床反应器气力进料特性的影响。试验结果表明：流化气速和喷动气速的增加均会提高进料率;流化气使床料流化并为落叶松颗粒提供进料空间,喷动气为落叶松颗粒提供动能,并平衡一部分床层压力;落叶松与石英砂粒径的增加对进料效果不利;流量比在1.9~2.7范围内进料率高且稳定性好。本文构建了生物质、床料与气体的三相流物理及数学模型,开展试验对模型进行验证,结果表明其预测误差为±13%。     

An experimental reactor for kinetic studies: continuously-fed batch reactor

The use of a continuously-fed batch reacter (CFBR) as an experimental tool for the kinetic studies is presented for liquid- and gas-phase reactions, and noncatalytic gas-solid reactions. An experimental CFBR run is demonstrated using the reaction involving sucrose conversion to substantiate the theoretical results. The concept used for the CFBR is the fact that at an extremum of concentration the rate of concentration change is zero. For the liquid- and gas-phase reactions, the CFBR can be used as an alternative to the CSTR. For slow reactions, the rate determined from a CFBR run is more accurate than the rate determined from a CSTR run. Determination of the rates over the entire conversion range is made easy for fast reactions with the use of the CFBR. Results are extended to noncatalytic gas-solid reactions. It is shown that the fractional change of reacting surface area of the solid reactant can be obtained using the CFBR under the limiting condition of negligible effect of mass transfer.     

Experimental and Theoretical Investigation of Double Gas Hydrate Formation in the Presence or Absence of Kinetic Inhibitors in a Flow Mini‐Loop Apparatus

Double gas hydrate formation in the presence or absence of kinetic inhibitors in a flow mini‐loop apparatus was investigated. For the prediction of the gas consumption rate during hydrate formation in this system, the rate equation based on the Kashchiev and Firoozabadi model for simple gas hydrate formation in a batch system was developed for double gas hydrate formation in a flow mini‐loop apparatus. To complete the theoretical evaluation of gas hydrate formation through the mini‐loop apparatus in the presence or absence of kinetic hydrate inhibitors (KHI), a laboratory flow mini‐loop apparatus was set up to measure the induction time for hydrate formation and the uptake rate when a gaseous mixture (such as 75 % C1/25 % C3, 25 % C1/75 % C3, 75 % C1/25 % i‐C4, and 25 % C1/75 % i‐C4) is contacted with water containing or not containing dissolved inhibitor under suitable temperature and pressure conditions. In each experiment, a water blend saturated with gas mixture was circulated up to the required pressure. The pressure was maintained at a constant value during the experimental runs by means of a required gas mixture make‐up. The effect of pressure on gas consumption during hydrate formation was investigated in the presence or absence of polyvinylpyrrolidone (PVP) and L ‐tyrosine as kinetic inhibitors at various concentrations. A good agreement was found between the predicted and experimental data in the presence or absence of KHI. The total average absolute deviation percents between the experimental and predicted values of gas consumption were found to be 16.4 and 17.5 % for the double gas hydrate formation in the presence or absence of the kinetic inhibitors, respectively.     

A new kinetic model for titanium dioxide mediated heterogeneous photocatalytic degradation of trichloroethylene in gas-phase

This paper focuses on the kinetics of photocatalytic removal and carbon mineralization of gaseous trichloroethylene (TCE) on near-UV irradiated TiO₂ Degussa P25. Experiments were carried out in a flat-plate photoreactor at TCE inlet concentrations of 100–500 ppmv, relative humidities (RH) of 0–62% and gas residence times of 2.5–60.3 s. Gas residence time distribution (RTD) curves revealed an axial dispersed plug flow in the photoreactor with Peclet numbers above 59.4. For all experimental conditions, the carbon mineralization efficiency (5.1–73.0%) was lower than the removal efficiency (8.6–99.9%) and dichloroacetylchloride (DCAC) was detected as a gas-phase degradation product. TCE removal efficiencies increased with lower TCE inlet concentrations, lower RH and higher gas residence times. Evaluating different kinetic models by least squares analysis, it was shown that the Langmuir–Hinshelwood (LH) model could not give an adequate fitting to the experimental results. A new kinetic model, explicitly taking into account electron–hole pair reactions, was developed based on linear TCE adsorption–desorption equilibrium and first order reaction kinetics. The new kinetic model described the experimental results in a more accurate way, as exemplified by a more randomly distributed set of residuals and by a reduction of the sum of squares (SSQ) by a factor 1.7–8.5. The effect of TCE gas-phase concentration, RH and light intensity on adsorption–desorption kinetics, electron–hole concentrations and chemical conversion rates is discussed.     

Mass Spectrometric and Bio-Computational Binding Strength Analysis of Multiply Charged RNAse S Gas-Phase Complexes Obtained by Electrospray Ionization from Varying In-Solution Equilibrium Conditions

We investigated the influence of a solvent’s composition on the stability of desorbed and multiply charged RNAse S ions by analyzing the non-covalent complex’s gas-phase dissociation processes. RNAse S was dissolved in electrospray ionization-compatible buffers with either increasing organic co-solvent content or different pHs. The direct transition of all the ions and the evaporation of the solvent from all the in-solution components of RNAse S under the respective in-solution conditions by electrospray ionization was followed by a collision-induced dissociation of the surviving non-covalent RNAse S complex ions. Both types of changes of solvent conditions yielded in mass spectrometrically observable differences of the in-solution complexation equilibria. Through quantitative analysis of the dissociation products, i.e., from normalized ion abundances of RNAse S, S-protein, and S-peptide, the apparent kinetic and apparent thermodynamic gas-phase complex properties were deduced. From the experimental data, it is concluded that the stability of RNAse S in the gas phase is independent of its in-solution equilibrium but is sensitive to the complexes’ gas-phase charge states. Bio-computational in-silico studies showed that after desolvation and ionization by electrospray, the remaining binding forces kept the S-peptide and S-protein together in the gas phase predominantly by polar interactions, which indirectly stabilized the in-bulk solution predominating non-polar intermolecular interactions. As polar interactions are sensitive to in-solution protonation, bio-computational results provide an explanation of quantitative experimental data with single amino acid residue resolution.     

Fluid catalytic cracking: Selectivity and product yield patterns

Fluid catalytic cracking, a common secondary process employed in the petroleum industry, is used to convert heavier feedstocks into products such as liquefied Petroleum Gas (LPG), motor gasoline, diesel etc. The present study focuses on developing a three lump fraction kinetic model to estimate the yield of C5 up to 370°C cut (motor gasoline and middle distillates). A Micro Activity Test (MAT) apparatus was used to estimate the parameters in the kinetic model. The study is useful in evolving a procedure to simulate plant performance using experimental data obtained in the MAT apparatus for a particular catalyst and feedstock in terms of the product yield pattern.