Simulation and Experimental System Terner Aseton-Butanol-Ethanol with Batch Distillation

Result of Aseton-Butanol-Ethanol (ABE) terner system simulation (ABE) in the form of temperature profile, liquida composition profile and vapour in bottom utilized as reference in ABE terner system experiment, with komparasi result of ABE terner system experiment and simulation will know how far deviation obtained. For the dissociation of ABE terner system done by research simulationly before done by research experimentally, so that in determination of research variable can more directional and expense of cheaper research. Simulation of ABE terner system by batch distillation use rigorous method, model DAEs and Matlab Ianguage. Result of from ABE terner system simulation later then comparation use Metanol-Ethanol-Propanol (MEP) terner system which forming homolog deret. Usage of MEP terner system in ABE terner system comparation, because MEP terner system mixture prediction form zeotropik mixture. Result of simulation in the form of temperature profile, liquida composition profile and vapor composition profile function of time dimensionless () either in bottom and also[in distilate. Is afterwards done by ABE terner system experiment with operating pressure 1 atmospher, ABE mixture volume 350 ml, ABE feed composition : 0.8, 0.1, 0.1 ( mole fraction) and : 0, 1, 2,3. Result of ABE terner system simulation comparation with MEP terner system come near result which same and show zeotropik mixture. Result of experiment and simulation in the form of temperature profile, liquida composition profile and vapor composition profile time dimensionless function either in bottom and also in distilate show result come near is samely. So that ABE terner system simulation after comparation with MEP terner system can wear by reference in ABE terner system experimen

Practical residue curve map analysis applied to solvent recovery in non-ideal binary mixtures by batch distillation processes

Batch distillation inherent advantages has initiated recent search for process feasibility rules enabling the separation of azeotropic or difficult zeotropic binary mixtures thanks to the addition of an entrainer. A systematic procedure enabling to find suitable process and eventually suitable entrainer for the separation of zeotropic or azeotropic binary mixture is described. It brings together into practical use batch distillation process feasibility rules, chemical affinity insight and thermodynamic data analysis available in the literature. The procedure has been implemented in a wizard computer tool and is illustrated on the separation of the water – acetonitrile binary homoazeotrope. Through this tool, all possible 224 feasibility rules and 326 batch distillation sequence processes are checked systematically for each entrainer

Entrainer selection for pressure swing batch distillation

The feasibility of the separation of binary homoazeotropes with pressure swing batch distillation by the application of an entrainer is studied. The feasibility studies are based on the assumption of maximal separation and on the analysis of batch distillation/stripping regions and the vessel path in the residue curve map of the ternary mixture. The following configurations are investigated: batch rectifier, batch stripper, double column batch rectifier and double column batch stripper. Rules for the selection of an entrainer are suggested

Heterogeneous Batch Distillation Processes: Real System Optimisation

In this paper, optimisation of batch distillation processes is considered. It deals with real systems with rigorous simulation of the processes through the resolution full MESH differential algebraic equations. Specific software architecture is developed, based on the BatchColumn® simulator and on both SQP and GA numerical algorithms, and is able to optimise sequential batch columns as long as the column transitions are set. The efficiency of the proposed optimisation tool is illustrated by two case studies. The first one concerns heterogeneous batch solvent recovery in a single distillation column and shows that significant economical gains are obtained along with improved process conditions. Case two concerns the optimisation of two sequential homogeneous batch distillation columns and demonstrates the capacity to optimize several sequential dynamic different processes. For such multiobjective complex problems, GA is preferred to SQP that is able to improve specific GA solutions

Feasibility of extractive distillation process variants in batch rectifier column

A systematic comparison is presented about the separation tasks of azeotropic and close-boiling mixtures applying batch extractive distillation (BED) in rectifier. All the eight possible mixture types with at most a single azeotrope (minimum and maximum boiling azeotropes with heavy, light, and intermediate boiling entrainers; and close boiling mixtures with heavy and light entrainers) are compared. The main results of the feasibility studies on the hitherto unpublished cases are presented. All the cases are feasible in batch rectifier, applying BED. The operation steps are determined by the relative position of the azeotropic composition and entrainer in bubble point ranking. The main limiting parameters (F/V, N, Epremix) are also determined by the mentioned relative position; only the existence of maximum number of stages in the rectifying section is determined by the type of the azeotrope. Use of residue curves maps (RCMs) for predicting feasibility is not generally satisfactory, but profiles maps can be used instead. Studying only the total reflux case can be misleading, and should be treated with great care. The theoretical results of separation variants applying intermediate boiling entrainer were proved experimentally

Separation of n-hexane - ethyl acetate mixture by azeotropic batch distillation with heterogeneous entrainers

In this article, a systematic study of the separation of the n-hexane - ethyl acetate mixture with an entrainer by heterogeneous azeotropic batch distillation is performed. Based upon the thermodynamic behaviour of the ternary mixtures, potential entrainers partially miscible with one or two original azeotropic components are chosen. In all cases, the entrainer adds a heterogeneous binary or ternary azeotrope that is the lowest boiling point in the ternary diagram. Therefore, it leaves the column by the overhead stream which is subcooled to get two liquid phases in the decanter. The phase with the highest amount of the original component is removed as distillate product whereas the entrainer – rich phase is continuously refluxed to the column. Considering methanol, acetonitrile, water and nitromethane as heterogeneous entrainers, screening was performed based on the composition of the unstable heteroazeotropic mixture, the ratio of both liquid phases in the condensed top vapour and the purity of the distillate product determined by the liquid – liquid envelope at the decanter temperature. The process feasibility analysis is validated by using rigorous simulation with the batch process simulator ProSimBatch. Simulation results are then corroborated in a bench experimental column for the selected entrainer, showing several advantages of heterogeneous batch distillation compared to homogeneous systems

Heterogeneous Extractive Batch Distillation of Chloroform - Methanol – Water : Feasibility and Experiments

A novel heterogeneous extractive distillation process is considered for separating the azeotropic mixture chloroform – methanol in a batch rectifying column, including for the first time an experimental validation of the process. Heterogeneous heavy entrainer water is selected inducing an unstable ternary heteroazeotrope and a saddle binary heteroazeotrope with chloroform (ternary diagram class 2.1-2b). Unlike to well-known heterogeneous azeotropic distillation process and thanks to continuous water feeding at the column top, the saddle binary heteroazeotrope chloroform – water is obtained at the column top, condensed and further split into the liquid – liquid decanter where the chloroform-rich phase is drawn as distillate. First, feasibility analysis is carried out by using a simplified differential model in the extractive section for determining the proper range of the entrainer flowrate and the reflux ratio. The operating conditions and reflux policy are validated by rigorous simulation with ProSim Batch Column® where technical features of a bench scale distillation column have been described. Six reproducible experiments are run in the bench scale column matching the simulated operating conditions with two sequentially increasing reflux ratio values. Simulation and experiments agree well. With an average molar purity higher than 99%, more than 85% of recovery yield was obtained for chloroform and methanol

New double column system for heteroazeotropic batch distillation

A new double column system (DCS) operated in closed mode is suggested for heterogeneous batch distillation. This configuration is investigated by feasibility studies based on the assumption of maximal separation and is compared with the traditional batch rectifier (BR). We study the configurations also by dynamic simulation based on a detailed model using a professional simulator. For the new configuration the minimal duration of the process is determined. The influence of the most important operational parameters is studied. The calculations and the simulations are performed for a binary (n-butanol–water) and for a ternary heteroazeotropic mixture (isopropanol–water + benzene as entrainer). One of the advantages of the DCS is that distillation of binary and ternary systems is performed in only one step. Furthermore the recovery of components is usually higher and the amount of byproducts is lower

Generalised model for heteroazeotropic batch distillation with variable decanter hold-up

A general model of batch heteroazeotropic distillation is proposed. Both liquid phases present in the decanter can be refluxed or withdrawn as distillate, their hold-up can be increased, decreased or kept constant, as well. By assuming maximal separation, that is, that the composition of the condensate always equals to that of the heteroazeotrope, the still path equation was derived. The still path directions are determined for all the 16 possible operational policies. It is possible to steer the still path in a desired direction by changing the operational parameters, which allows the recovery of a pure component in the still. The still path directions are validated by rigorous simulations for three policies not published yet using the mixture water – formaldehyde – propyl formate. From the 16 operational policies, 11 can be considered as useful in practice. To demonstrate the advantage of using a non-traditional policy, the separation of the mixture aniline – ethylene glycol – water was investigated, as well. By using a non-traditional operational policy with hold-up reduction in the decanter a higher purity of ethylene glycol was obtained in the still

Bottleneck-based heuristic for permutation flowshop scheduling

The newly heuristic is developed by introducing the bottleneck-based concept that was applied at the beginning of initial solution determination. The heuristic is known as Bottleneck-Based (BNB) heuristic. The previous study found that the scheduling activity become complex when dealing with large number of machine, m > 2, it is NP-hardness. Thus, the main objective of this study are to propose and develop a new heuristic for solving permutation flowshop scheduling by considering four-machines and n-jobs (n = 6, 10, 15, 20). Three phases were applied into this study in order to boost the makespan performance of the proposed heuristic. Two phases (bottleneck identification phase and initial sequence arrangement phase) were newly introduced and combined with the existing famous Nawaz, Enscore and Ham (NEH) insertion technique. There are four potential dominant machines (M1, M2, M3, M4) clustered as bottleneck machines. A total 1000 set random processing time for each job sizes was tested using Excel simple programming with built in Visual Basic for Application (VBA). The heuristic performance was evaluated based on the average makespan ratio, average percentage error, and percentage of solution performance obtained. This study considered the NEH heuristic as the best and appropriate tool for comparison purpose since NEH heuristic is the best performing heuristic in minimizing the makespan. The heuristic evaluation result showed that the BNB heuristic is performing better than the NEH at bottleneck machines M1, M3 and M4. While, heuristic verification result showed that the bottleneck algorithms performed the best in minimizing the makespan for set of problems with bottleneck machine M4. However, the overall result showed fluctuate values over the size of jobs. The result of this study shown that the developed BNB heuristic achieved good performance in solving small sized problems however further modification is needed for medium and large sized problems