硅油光-热老化气升式反应器数值模拟

为进行液浸聚光光伏系统中液浸液体即二甲基硅油在光热条件下的老化实验研究,设计制作了气升式外环流光催化反应器。采用Fluent软件欧拉多相流模型和RNG k-ε湍流模型对反应器进行了三维全尺寸数值模拟。分析了结构参数、操作参数和硅油物性参数对反应器中气液两相流动的影响,得到反应器内循环液速和气含率等参数的分布。模拟结果与实验结果有较好的一致性。模拟结果表明:硅油黏度越小,循环液速越大,气含率越小;反应器适宜操作气速不应大于0.02 m/s;反应器最适宜高径比和环隙面积比分别为47.6和0.31~0.41。     

多层气提式气、液、固三相反应器的研究

本文发展了多层气提式气、液、固三相反应器。研究了它的溢流管的稳定性,测定了液泛速度,并建立了一个计算液泛速度的经验方程式。 在连续流动的多层气提式反应器中进行了氨性溶液浸取氧化铜矿及碳酸化浸取钢渣提钒的试验。在间歇实验的基础上可以利用CSTR模型模拟连续流动的实验结果。 这种装置已成功地应用于工业性生产试验的设备上。     

The gas–liquid contacting effect on the operation of small scale upflow hydrotreaters

The effect of reactor geometry and bed dilution on the extent of gas oil hydrodesulfurization was tested by conducting hydrodesulfurization experiments in two laboratory reactors of different scale with non-diluted and diluted beds in ascending flow. The superficial gas and liquid velocities and the catalyst bed height were kept constant while the main difference between the two reactor scales was the reactor diameter. The diluted bed of the mini-reactor showed the best performance and its results were identical in upflow and downflow mode. The differences between the performance of the mini- and the bench-scale reactor operating in upflow mode have been investigated. Reactor performance simulation was attempted by a mathematical model that takes into account axial dispersion of the liquid phase and gas–liquid mass transfer. Bench-scale reactor operation was characterized by lower mass transfer rates than the corresponding mini-scale one. Combining model predictions and mock up operation it is concluded that the stronger mass transfer resistances calculated for the bench-scale reactor are associated with poorer gas distribution through the catalyst bed. Reduction of the bed diameter results in better gas–liquid contact by forcing the gas bubbles to distribute more effectively into the liquid phase.     

Optimization of reagents injection in a stirred batch reactor by numerical simulation

Computational fluids dynamic was used to analyze the mixing operation within a stirred batch reactor to distribute rapid and homogeneously reagents, used in the refining process of liquid lead. The flow pattern and distribution of the reagents inside the reactor were analyzed through tracer response curves obtained by numerical simulation.The predominant mechanism of momentum and mass transfer for macro-mixing is convection for the mean and eddy flows. Based on the assumption that the tracer is distributed in the vessel by convection and diffusion, the dynamic distribution of the tracer concentration inside the stirred batch reactor was calculated by solving the Reynolds-averaged conservation equations and the Realizable κ–ɛ turbulence model. The mean and tracer flow was considered as incompressible, isothermal and single phase under turbulent conditions.To optimize the injection point of reagents in the stirrer batch reactor, several simulated tracer concentration curves were obtained from monitoring points located at different radial and axial positions.     

STUDIES ON GAS-LIQUID-SUSPENDED SOLID MULTIDECK GAS LIFT REACTOR

Following the work on gas lift reactor (Pachuca tank) for gas-liquid-suspended solid 3-phase reaction,multideck gas lift reactors have been developed.This type of reactor has many unique advantages suchas realization of counter-current operation between gas and slurry,reduction of gas consumption and lower-ing of the amount of volatile components of the liquid which has to be recovered from the exit gas.The stability of the overflow tube of the reactor was studied.A semiempirical equation was derived tocalculate the flooding point of the reactor.The operating range of the overflow tube was also deter-mined.This multideck reactor has been operated successfully in a pilot plant of ammonia leaching of copperore.Results agree reasonably well with those predicted from small scale batch experiments.The extractionof vanadium from soda roasted steel slag in a 5-deck reactor with carbon dioxide in the gas phase wasalso satisfactory.Experimental results obtained from the continuous flow 5-deck reactor and those calcu-lated from batch experimental data with CSTR model were in agreement.     

Operation characteristics of a new liquid-solid circulating moving bed reactor

The liquid-solid circulating moving bed reactor is a novel one, which consists of two or more reaction chambers and a particle transport system. Particles move down to the lower reaction chamber from the upper reaction chamber through an upper conduit and to the particle transport system through a lower conduit, and then are conveyed into the upper reaction chamber through a riser. The circulating rate of particles and the flow of liquid in the two conduits are key factors to the continuous steady operation of the reactor; they can be controlled by varying operating conditions: the outlet liquid flow rate in the regeneration chamber, the outlet liquid flow rate in the reaction chamber, the inlet liquid flow rate of the reactants, and the flow rate of driving flow. A flow model has been proposed to quantify the operation characteristics of the reactor. The results predicted by the model show satisfactory agreement with the experimental data.     

OPERATION CHARACTERISTICS OF A NEW LIQUID-SOLID CIRCULATING MOVING BED REACTOR

The liquid-solid circulating moving bed reactor is a novel one, which consists of two or more reaction chambers and a particle transport system. Particles move down to the lower reaction chamber from the upper reaction chamber through an upper conduit and to the particle transport system through a lower conduit, and then are conveyed into the upper reaction chamber through a riser. The circulating rate of particles and the flow of liquid in the two conduits are key factors to the continuous steady operation of the reactor; they can be controlled by varying operating conditions: the outlet liquid flow rate in the regeneration chamber, the outlet liquid flow rate in the reaction chamber, the inlet liquid flow rate of the reactants, and the flow rate of driving flow. A flow model has been proposed to quantify the operation characteristics of the reactor. The results predicted by the model show satisfactory agreement with the experimental data.     

气液固三相循环流化床气液传质行为

<正>气液固三相流化床反应器在石油化工、湿法冶金、环境工程和煤的液化等工业领域得到了广泛应用,其基础研究也取得了很大进展.但是,传统三相床主要应用于低液速(U_L<     

对二甲苯氧化反应器非均匀混合模型

对二甲苯氧化是一个复杂的气-液-固三相反应过程。今根据实验测取的对二甲苯氧化反应动力学关系与数据,建立了工业氧化反应器的非均匀混合模型,用以考察气、液相的混合状况及其对反应的影响。模型采用三区串联加区问返混的结构,区间返混参数由工业反应器实测轴向温度分布拟合确定。计算表明,釜内液相混合接近全混、流,而气相氧浓度存在明显的轴向梯度：溶剂蒸发与液相混合相互竞争造成反应器内有一定的温度梯度：氧浓度梯度和温度梯度共同作用使得CO2．CO量增多,燃烧副反应加剧,这其中氧浓度梯度起主要作用。     

Evaluation of the three phase transport reactor

A high aspect ratio chemical reactor for reacting a liquid with a gas in the presence of a finely divided catalyst was tested. The gas was sparged into the bottom of a tubular reactor with the slurry of liquid and catalyst flowing countercurrent to the gas. The liquid phase hydrogenation of alpha-methylstyrene to cumene on a Pd. catalyst was studied in semibatch operation of the reactor with slurry recycle. The reacor was 1 1/2-in. I.D. by 6-ft. long. The following variables were studied at a temperature of 28°C and a pressure of 1 atm: superficial gas velocities of 1.1 to 3.3 cm/sec., and catalyst loadings from 0.4 to 2.0 gm. catalyst per liter. A model of the reactor was developed and successfully compared with the data.     

A recycle reactor for measuring hydrogen isotope exchange kinetics under vapour phase and trickle bed conditions

A recycle reactor system has been developed to measure the activities of catalysts for isotope exchange between hydrogen gas and water vapour. To allow testing of reasonably large quantities of catalysts, the reactor was operated with a high recirculating flow of hydrogen gas passing through a saturator to provide the water vapour required for the reaction. In this mode of operation, only a small spiking gas flow was required as feed compared to the very high feed flow that would be required for once-through operation. The reactor was also operated as a trickle bed by recirculating the saturator water. By testing catalysts under both vapour and trickle bed modes, it was possible to investigate the effect of trickling water over the catalyst on the catalytic activity. Kinetic exchange rates under vapour phase operation were calculated from both plug flow and well-mixed reactor models. The former model was found to be the appropriate one for the ranges of operating conditions investigated. However, for trickle bed operation, the well-mixed reactor model was found to be the suitable one. Vapour phase and trickle bed tests done with random bed and structured bed catalysts indicated that the gas phase isotope exchange reaction was not impaired by the presence of liquid water in the reactor.     

Unsteady-state operation of trickle-bed reactor for dicyclopentadiene hydrogenation

Unsteady-state operation of a trickle-bed reactor (TBR) was investigated using a multi-step exothermic reaction, hydrogenation of dicylcopentadiene (DCPD) in the presence of Pd/Al₂O₃ catalyst. The influences of five operation strategies on the reactor performance were symmetrically studied and compared with the steady-state operation, including ON-OFF and PEAK-BASE modulations of the liquid flow rate or concentrations, and a novel hybrid modulation of liquid flow rate and concentration. Attempts were also made to develop an unsteady-state operated TBR model based on a plug-flow model incorporating fluid flowing behaviors, three-zone partial wetting catalyst, vapor-liquid phase equilibrium and enthalpy balance, to predict the overall performance under unsteady-state operations. Compared with the experimental observations, it is indicated that the developed model is generally reliable to predict performance enhancement for different modulation strategies.     

AISI 304 L stainless steel decontamination by a corrosion process using cerium IV regenerated by ozone Part II: Process optimization

Empirical and analytical approaches were used to model a pre-industrial pilot reactor to optimise a new decontamination process for AISI 304 L stainless steel. The alloy corrosion rate was modelled as an analytical function of the total cerium content and the ozone flow injected in the reactor. The empirical model of the corrosion rate, obtained by gravimetry, takes into account all the parameters, including the kinetics of alloy grains detached from the metal by intergranular corrosion. The discrepancy observed between the analytical and empirical models was explained by a two-step corrosion process. The dimensions and quantity of grains falling in the liquid were at first both underestimated. The study showed that the grains had to be extracted continuously from recirculating liquid in the future industrial reactor.     

液体喷射单相环流反应器周期振荡操作模拟

<正>液体喷射单相环流反应器在化学和生化工程中应用较多。有关其流动特性,Blanke已作了较为全面的综述。一般这种反应器的操作采取中心或环隙喷射的定态方式,Douglas和Baird等对反应器的研究认为,传统的定态操作并不能保证过程总处于最佳状态,在某些情况下进行非定态的振荡操作,可能更有利于反应和传递,其中确定合适的振荡周期是实现这一目的的关键。文献[5,6]利用内环流反应器中心气升和环隙气升的周期切换,实现了环流反应器的振荡操作,并较有效地提高了反应器溶氧传质系数。将这种操作方式用于面包酵母的培养,可增加细胞收率。环流反应器振荡操作时流体流动的特点不单表现为流动处于非定态,而且当喷射位置从中心切向环隙或相反时,流体流动方向都要反向变化一次。因此     

A porous carbon membrane reactor for the homogeneous catalytic hydration of propene

A porous carbon membrane contactor was studied to determine whether such a reactor could be used for homogeneous catalytic reactions. The hydration of propene, catalysed by an aqueous solution of phosphoric acid, was selected as a suitable model reaction. Experiments at high pressure and temperature were conducted in a laboratory-scale gas phase continuous reactor equipped with a flat carbon membrane contactor. It was shown that reasonably stable operation of the reactor could be achieved at high operating pressures by tailoring the porous structure of the carbon membrane and coupling the reactor with an on-line feedback pressure controller. The reactor operated in a mass transfer limited regime due to mass transfer resistance in the liquid filled membrane pores. Periodic oscillation of transmembrane pressure was shown to reduce mass transfer resistance and considerably improve the overall reactor performance.A dynamic model of the reactor was developed and the results of simulations compared favourably with experiments and the performance of a commercially operated conventional reactor employing a supported liquid phase (SLP) catalyst.     

Catalytic performance improvement of styrene hydrogenation in trickle bed reactor by using periodic operation

We investigated the catalytic performance improvement of styrene hydrogenation in a trickle bed reactor by using periodic operation. The effects of cycle period and split on relative conversion, which is defined as styrene conversion obtained from periodic operation over that from steady state operation, were examined at various operating conditions including gas and average liquid flow rates, pressure and temperature. The experimental results reveal that both cycle period and split have strong influence on the catalytic performance. The fast mode (short cycle period) is a favorable condition. The improvement by the periodic operation becomes less pronounced for operations at high average liquid flow rate, pressure and temperature. From this study, a maximum improvement of styrene conversion of 18% is observed.     

A STUDY ON THE PERFORMANCE OF THE CATALYTIC POROUS-WALL THREE-PHASE REACTOR

A theoretical investigation of a catalytic porous-wall reactor in which gaseous and liquid reactants approach each other from opposite sides of the catalyst is undertaken. Equations for the annular liquid-channel are coupled with those for the catalytic wall and solved numerically and analytically using a simplified model. For the model reaction under study, the main design and operation parameters which affect reactor performance are the Thiele modulus, Peclet number, width of the liquid channel and the inlet concentration of the reactant in the liquid phase.

The effect of reactor configuration is peculiar to the cylindrical geometry because the thickness and relative location of the catalytic wall as well as the selection of the liquid and gas channels can influence the reactor performance. Thin-walled catalyst tubes have larger effectiveness factors and as the tube radius approaches that of the reactor, conversion in the reactor increases especially when the liquid is saturated with the gaseous reactant. Concentration of the liquid reactant in the feed has a significant effect if the reactant is depleted at some point inside the catalyst wall. Since the reaction zone width can be adjusted by changing the feed composition, this might have important implications with respect to selectivity.     

料浆法磷铵料浆二次氨中和生产磷酸二铵的研究

在实验模试装置上，研究了料浆法浓缩料浆二次氨中和生产磷酸二铵（ＤＡＰ）管式反应器的结构特性，建立了该反应器的液相返混参数Ｐｅ表达式和体积传质系数ＫＧａ的计算式。据此设计的管式反应器，在３万吨／年ＭＡＰ装置上生产ＤＡＰ，经７２ｈ运行考核，生产稳定可靠，达到了预定目标。     

Mass transfer in trickle-bed reactors at low reynolds number

Mass transfer rates were determined in a 3.4 cm i.d. trickle-bed reactor in the absence of reaction by absorption measurements and in presence of reaction. Gas flow rates were varied from 0-100 l/h and liquid flow rates from 0-1.5 l/h. The catalyst particles were crushed to an average diameter of 0.054 and 0.09 cm. Mass transfer coefficients remained unaffected by change in gas flow rate but increased with liquid rate. The data from absorption measurements were evaluated with predictions based upon plug-flow and axial dispersion model. Mass transfer coefficients were found greater in case of axial dispersion model than that of plug-flow model specially at low Reynolds number (Re₁ < 1).Hydrogenation of α-methylstyrene to cumene using a Pd/Al₂O₃ catalyst was taken as a model reaction. Intrinsic kinetic studies were made in a laboratory-stirred-autoclave. Mass transfer coefficients were determined using these intrinsic kinetic data from the process kinetic measurements in trickle-bed reactor. Mass transfer coefficients under reaction conditions were found to be considerably higher than those obtained by absorption measurements.Correlations were suggested for predicting mass transfer coefficients at low Reynolds number.The gas to liquid mass transfer coefficients for lower gas and liquid flow rates were determined in a laboratory trickle-bed reactor. The effect of axial dispersion on mass transfer was considered in order to evaluate the experimental data. Three correlations were formulated to calculate the mass transfer coefficients, which included the effect of liquid loading, particle size and the properties of the reacting substances. The gas flow rate influences the gas to liquid mass transfer only in the region of low gas velocities. In the additional investigations of gas to liquid mass transfer without reaction in trickle-bed reactor, the mass transfer coefficients were determined under reaction conditions and the intrinsic kinetics was studied in a laboratory scale stirred autoclave with suspended catalyst. A few correlations are formulated for the mass transfer coefficients. A comparison with the gas-liquid mass transfer coefficient obtained by absorption measurements showed considerable deviations, which were illustrated phenomenologically.     

Comparison of two-phase upflow and downflow fixed bed reactors performance: Catalytic SO2 oxidation

A time- and space-dependent model based on the piston-dispersion-exchange model for liquid flow was developed to analyze the performance of two-phase upflow and downflow fixed bed reactors and was applied to the catalytic SO₂ oxidation. The hydrodynamic parameters were determined from residence time distribution measurements, using an imperfect pulse method for time-domain analysis of nonideal pulse tracer response. A transient diffusion model of the tracer in the porous particle coupled with the PDE model was used to interpret the obtained RTD curves. Gas-liquid mass transfer parameters were determined by a stationary method based on the least square fit of the calculated concentration profiles in gas phase to the experimental values. It is shown that two-phase downflow fixed bed reactor performs better at low liquid flow rates, while two-phase downflow fixed bed reactor performs better at low liquid flow rates, while two-phase upflow performs better at high liquid flow rates.