There are many computer algorithms available for performing multicomponent distillation calculations,however,most of them are rating type algorithms(i.e.the number of equilibrium stages,reflux ratio,loca-tions of feeds,side—draws and intermediate reboilers are fixed in the calculation),they are not suitable fordesigning a new column.In this work,the authors have proposed a new design algorithm by applying optmization techniques.Based on the specified separation requirements and the chosen criterion of optimization,a set of optimumparameters can be determined through a single calculation.A hybrid method(tridiagonal matrix and 2N Newton-Raphson)was used in the rigorous distillationcalculation loop,and thermodynamic model(BWRS or PR)was coupled for performing VLE and enthalpycalculations.This new algorithm has been tested on five typical complex fractionating columns(including three fieldoperating columns),close agreements with original design parameters were observcd.

The adsorption of Me(metal),NH_3 and CO_2 on lignite from ammoniacal solution containing metallicions such as Cu,Ni,and Co was investigated.Preliminary mechanism studied revealed that active carboxyland phenolic groups of humic acid in lignite as well as surface adsorption were involved.The rate of ap-proach to adsorption equilibrium on lignite was NH_3>Ni>Co>Cu andthe adsorption on lignite is Cu>Co>Ni>NH_3.The order of selective elution was NH_3>>Ni,Co>Cu.All metals were fully stripped and NH,could only be recovered partially.NH_3 adsorbed on lignite fron metal-ammoniacal solution is easily lost by volatilization,only a smallfraction remaining on lignite at a temperature of 120℃.CO_2 adsorbed physically in nature from ammonia-cal solution with a capacity of less then one percent was observed under the practical conditions generallyin hydrometallurgy.

The dehydrogenation of tetralin over Ni-Mo/A1_2O_3,Fe_2O_3/Al_2O_3,Fe_2O_3 and FeS_2 has been shown inthis investigation to be a typical consecutive reversible reaction,with a small amount of 1,2-dihydronaph-thalene as an intermediate.On the less active catalyst Fe_2O_3,a few percent of 1,4-dihydronaphthalene(DHN)is also formed—the more active the catalyst,the lower the concentration of DHN.The rate of dehydrogena-tion rises with an increase of the partial pressure of tetralin,and declines with an increase of the partialpressure of hydrogen.It was observed that DHN is much more active than tetralin and naphthalene,andin the presence of a catalyst,it can be converted rapidly into naphthalene and tetralin.The fact that hydrogencan accelerate the hydrogenation of DHN is thought to be the main reason for its inhibiting the dehydroge-nation of tetralin.In the presence of a catalyst,1,4-DHN it unstable and can be isomerized into 1,2-DHNvery fast.These different catalysts have almost the same order of activities for dehydrogenation of tetralin,conversion of DHN and hydrogenation of naphthalene.On the hypothesis that the reaction is a consecutiveone on the catalyst surface and that the adsorbed DHN is a very active intermediate,a reaction model hasbeen deduced.The equilibrium constants of adsorption and the rate constants of the catalytic reaction werecalculated.The curves so calculated fit the experimental data very well,thus showing the validity of thismodel.Certain experimental results were explained in the light of this model and the related parameters.

A kinetic model dC/dt=a+βC~(1/3)for suspension polymerization of vinyl chloride was developed.Kineticstudies on such polymerization were carried out in a stainless steel tube reactor in the presence of high-,medium-,or low-activity initiators at different concentrations,and at temperatures ranging from 50 to 62~C.Twenty-six sets of kinetic data were obtained under different conditions.According to these experimentalresults,the acceleration behavior of vinyl chloride polymerization was discussed in detail.It is proposed thatthe auto-acceleration effect is due to the decrease of the termination rate constnat in the polymer-rich phaseand to the increase of initiator concentration owing to volume contraction during polymerization with aninitiator of lower activity.All plots of dC/dt against C are nonlinear during the two-phase stage,while dC/dtversus C~(2/2)curves show much better linearity up to 60—70% conversion.The proposed model can beused to explain satisfactorily why the reaction order of initiators is between 0.5 and 1.0.

In this paper,the absorption with second-order irreversible chemical reaction in the film flow of non-Newtonian power law fluids was studied.The solution of several differential equations which portray abovephenomena was gotten and agrees well with our experimental data.

A new technique for measuring simultaneously adsorption rate and temperature variation in zeolite hasbeen developed.The transient temperature process during adsorption of gas on zeolite was analyzed by meansof a simple model.It was found that the diffusion of gas in zeolite crystallines could be made almost iso-thermal if the experimental conditions were appropriately designed.Thus the thermal effect on determinationof diffusion coefficient of gas in zeolite could be neglected.

The catalytically active components of a series of Fe_2O_3-Sb_2O_4 mixed oxide catalysts with differentSb/Fe ratio,calcined at elevated temperature,as well as with or without support,have been investigated byX-ray diffraction analysis,Mossauer spectroscopy and XPS in order to elucidate their catalytic behavior inammoxidation of propylene.Correlations of acrylonitrile yield with Fe~2+ and Fe~3+ respectively showed that,FeSbO_4 seems to bethe basic active component of catalyst,upon which the formation of new phase containing Fe~3+ is responsiblefor a good selective oxidation.

In this article a new arrangement of extraction cascade—multiple stage counter-current extraction processwith alternating extraction and stripping is presented.The effects of increasing mass-transfer rate and decreas-ing the number of extraction stage in an extraction process may be obtained by adopting this new arrange-ment.Extraction cascade calculation for two extraction systems-extraction of iron with N,N-bis-(l-methl-heptyl)acetyl amide(N-503)* and extraction of H_3PO_4 with DBSO has been carried out and the experi-ment has been done with the former system.The results of calculation and experiment show that the extraction efficiency increases significantly byadopting this new alternating arrangement,compared with a commun multiple stage counter-current process.The new alternating extraction and stripping arrangement may be called alternating extraction process.

It is found that the expression for(γ/x)_x-o derived on the basis of Lenoir’s works should Ix differentfrom that derived by Kikic and Renon in 1976.and(lnγ_1,/x_1)_x_1=0 values have beenmeasured for 10 binary systems by gas-liquid chromatography.According to the new expression,UNIQUACparameters and the vapor-liquid eqilibrium data are evaluated.Of the six systems data available in litera-ture the predicted results are satisfactory.

This paper describes a mathematical model and an algorithm which can be used for simulation of in-terlinked column systems consisting of liquid-liquid extraction and distillation.This algorithm is basedupon Newton-Raphson iteration technique using suitable damping factors and solutions of simplified modelas initial values of exact calculations.With the exception of principle specification it is possible to interchangethe iteration variables and/or noniteration variables with design variables to meet requirements of design.A process of recovery of phenol from waste water containing pheonol is illustrated to varify the model andalgorithm.The results are satisfied.

A new strategy of finding the best set of tear streams is proposed in this paper.It includes lining upall the nodes of the net in the declining order of node weights,and then adjusting the node positions in thesequence such that the total weights of the counter streams minimilcd.The finally formed node sequenceindicates the computation order of the nodes,and the still existing counter streams constitute the tear set.Neither loop identification nor excessive matrix operations are needed in this procedure;therefore,it hasbeen the simplest reliable method of net decomposition to data,and this is demonstrated by seven well-knownexamples.

In this paper,we consider the process development and scaling up of trickle-bed reactor for 1,4-butynediolsynthesis.Three laboratory chemical reactors have been used,i.e.,a batchwise stirred kettle for the de--termination of intrinsic kinetics,a continuous rotating basket reactor for macrokinetics of large catalystpellets,and an external recycle differential trickle-bed reactor for bed-kinetics under liquid flow rates of in-dustrial equipment.The kinetic data obatined from above three reactors can be correlated in power form rate equations,and the results not only present definite proof of the relationships between contacting effectiveness factorsand liquid flow rates developed by Satterfield,but also verify the influences of liquid flow rates under higherand lower temperatures.The external contacting effectiveness factors in trickle-bed reactor we determined can be used to correctthe macrokinetic models of catalyst pellets determined from rotating basket,and the corrected kinetic modelscan be checked by an adiabatic pilot equipment with rather successful results.