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Kordnejad M.,Shiraz University | Shokroo E.J.,The Parthia Chemistry Company | Shahcheraghi M.,The Parthia Chemistry Company
Petroleum and Coal | Year: 2013

Real Time Optimization (RTO) of industrial shell and tube methanol reactor is presented. Mathematical modeling of the reactor is considered as the case study. inlet concentrations of CO, CO2, H2, H2O and methanol are used as disturbances. Methanol output is maximized by adjusting the temperature of the shell as manipulating variable. Differential evolution (DE) and genetic algorithm are utilized for optimization purpose; in which the optimizer initiates every hour and determines the optimal shell temperature. Catalyst activity reduction is updated as model parameter every 24-hour periods. Comparing the optimization results demonstrates that DE algorithm requires less CPU time than genetic algorithm. Consequently, using the optimization algorithm and control loop, methanol production increases up to 15%. Source


Mofarahi M.,Persian Gulf University | Shokroo E.J.,The Parthia Chemistry Company
Petroleum and Coal | Year: 2013

The performances of two types of zeolite 5A and zeolite 13X in oxygen separation from air with a two-bed six-step pressure swing adsorption (PSA) system were investigated using mathematical modeling. The effects of feed flow rate, adsorption step pressure, adsorption step time and purge to feed ratio on oxygen purity and recovery are studied. Comparison of two types of zeolites shows that the PSA process performance (in terms of purity and recovery) was better with zeolite 13X than the zeolite 5A. Furthermore, Results of simulation indicated a very good agreement with some current literature experimentally work. Source


Shokrooi E.J.,The Parthia Chemistry Company | Shahcheraghi M.,The Parthia Chemistry Company | Farniaei M.,The Parthia Chemistry Company
Petroleum and Coal | Year: 2013

A one dimensional dynamic model for a riser reactor in a fluidized bed catalytic cracking unit (FCCU) for gasoil feed has been developed in two distinct conditions, one for industrial FCCU and another for FCCU using various frequencies of microwave energy spaced at the height of the riser reactor (FCCUMW). In addition, in order to increase the accuracy of component and bulk diffusion, instantaneous and overall fractional yield is used in a heuristic manner. Furthermore, the effect of various input temperatures on gasoline yield with FCCU-MW has been studied. The results of the convectional FCCU simulation show great compatibility with the plant data in hand. Comparison of the two models shows that microwave energy gives better results in terms of gasoline yield. Also it has been shown that the increase of feed temperature leads to the increase of gas oil conversion and especially gasoline yield. Source


Shokroo E.J.,The Parthia Chemistry Company | Shahcheraghi M.,The Parthia Chemistry Company | Farniaei M.,The Parthia Chemistry Company
Petroleum and Coal | Year: 2014

The Jam H2-PSA industrial plant, a five-bed PSA, is studied numerically by mathematical modeling and numerical simulation. The model includes energy, mass and momentum balances. The coupled partial differential equations are solved using fully implicit forth order Rung-Kutta scheme in the simulation. In general, the PSA process performance strongly influenced by the design parameters and operational variables. So, this could be achieves a maximum possible performance relate to an optimum amount of process variables. Therefore it is important that the behavior of the PSA operating variables were under take a review to knowing the optimum operating conditions. The Jam H2-PSA plant has been designed by the UOP co., so the design parameters is not being considered for review in this study. Since there are large feed temperature variations in the H2-PSA, in this work we are dealing with the feed temperature and investigation of its effect on the H2 purity and recovery known as a operating variable. Finally, the results of simulations show that the feed temperature near to range of 32-38 °c is well suited to H2 production in terms of its purity and recovery. In addition, as the feed temperature increases H2 productivity decreases. Source


Shokrooi E.J.,The Parthia Chemistry Company | Shahcheraghi M.,The Parthia Chemistry Company | Farrokhizadeh A.,The Parthia Chemistry Company | Farniaei M.,The Parthia Chemistry Company
Petroleum and Coal | Year: 2014

The Jam H2-PSA industrial plant, located in the southern pars zone of Iran, was studied numerically by mathematical modeling and numerical simulation. The major disadvantage of the steps sequence table of the Jam H2-PSA plant is the existence of a time-delay between two purge (PG) steps. In addition, the time of adsorption (AD) step does not equal to PG step. The existence of the timedelay in PG step and inequally in times of the pressurizing (PR) and depressurizing (BD) steps can be influenced on the process performance (mainly H2 recovery). In this work, therefore, a steps sequence table is designed in a way to take the same time for AD and PG steps and also same time for BD and PR steps. The two other characteristics of the designed sequence table are the continuity of the PG step and purging of a bed by two other beds effluent, in contrast to plant sequence table that two beds are regenerated by a bed effluent. Furthermore, the results of simulations show that the H2 recovery is improved with the proposed steps sequence table in this work. In addition, results of simulation indicated a very good agreement with plant data. Source

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