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This is our main download page for ChemSep containing updates for the latest LITE version as well as case stories and examples. This page is changing frequently.

File Description
[lite.exe] ChemSep-LITE, limited to 300 stages and 40 components with the equilibrium flash/column simulator and 400+ component library.
[lite.zip] ChemSep-LITE Zip-file installer

 Flowsheets that use ChemSep

We use COCO as tool for testing ChemSep columns in (petro)chemical process simulations. This free simulation tool is a great platform for students to become familiar with various commercial chemical processes and the simulation techniques required for design and optimization of chemical process plants.

Files Description
[fsd] [png] LPG Divided Wall Column NEW

LPG Divided Wall Column as described in December 2018 Gas Processing issue.

[pdf] [fsd] [png] ASU flowsheet ASU PFD ASU flowsheet by H.Kooijman (2006). Air Separation unit producing 60 t/h oxygen (recovery 75%) and liquid argon (recovery 85%) using a simplified flowsheet (i.e. refrigeration air is not compressed to a higher pressure, resulting in a lower efficiency, and the simple Peng-Robinson equation of state is used for simulation, leading to inaccuracies in the predicted refrigeration due to the JT effect).
[fsd] [png] Butyl acetate process Process to synthesize Butyl Acetate from Methyl Acetate and Butanol, adapted from Luyben et al., Ind.Eng.Chem.Res. (2011) 50 pp. 1247-1263. Note that the temperature of the last column has been increased to 4.4 atm to match the bottom temperature of the Butyl Acetate column. Also realize that the Methyl Acetate recycle rate is a strong function of the chosen thermodynamic models and their interaction parameters.
[fsd] [png] Cumene process Process for producing Cumene from Benzene and Propylene as adapted by Luyben in Ind.Eng.Chem.Res. (2010) Vol. 49 pp. 719-734. Note that this flowsheet uses fixed conversion rates in the reactor whereas the original publication uses rate equations.
[fsd] [png] Butanol Water heterogeneous distillation Separation of Butanol and Water by making use of the liquid-liquid-equilibria providing a means to break the vapor-liquid azeotrope, adapted from Luyben et al. Energy Fuels (2008) 22 pp. 4249-4258.
[fsd] [png] Pressure swing distillation Separation of the Methanol and Acetone minimum temperature azeotrope by using the pressure sensitivity of the azeotropic composition of this mixture by operating two columns at different pressures, adapted from Luyben et al. Ind.Eng.Chem.Res. (2008) 47 pp. 2696-2707.
[fsd] [png] Methanol from syngas Methanol synthesis from syngas as described by Luyben et al. Ind.Eng.Chem.Res. (2010) 49 pp. 6150-6163. Note that this flowsheet uses fixed conversion rates in the reactor whereas the original publication uses rate equations. Furthermore, the temperature of the vapor overhead recycle of the methanol column is highly dependent on the flowrate and thermodynamic model selection.
[fsd] [png] BTX Petlyuk / divided wall column BTX Petlyuk / Divided Wall Column as described by Luyben in Ind. Eng. Chem. Res. (2009) Vol. 48 pp. 6034-6049 simulated as one column.
[fsd] [png] Pervaporation (hybrid) distillation of ethanol and water Separation of Ethanol and Water using pervaporization to break the azeotrope. Note that the reflux ratio is set instead of the overhead composition because the sensitivity to the binary interaction parameters of the UNIQUAC model and the vapor pressure models. Specification of an 85% overhead would lower the reflux ratio to 2.5, lowering the condenser duty requirement. Adapted from Luyben, Ind.Eng.Chem.Res. (2009) 48 pp. 3484-3495.
[fsd] [png] THF / Water azeotropic distillation Pressure swing THF / Water azeotropic distillation with two columns operating at different pressures using heat integration, as described by Luyben in Ind.Eng.Chem.Res. (2008) Vol. 47 pp. 2681-2695.
[pdf] [fsd] [png] MCHT Extractive distillation of MethylCyloHexane/Toluene using Phenol adapted from Tiverios and Van Brunt in Ind.Eng.Chem.Res. (2000) 39, pp. 1614-1623
[fsd] [png] MA Extractive distillation of Methylal from Methanol using DMF as described by Wang et al. in Ind.Eng.Chem.Res. (2012) Vol. 51 pp. 1281-1292.
[pdf] [sep] Aromatics column described by R. Strigle (Gulf., 1987).
[pdf] [sep] Depropanizer described by R. Strigle (Gulf., 1987) to recover propylene and propane from C4 and heavier hydrocarbons.
[pdf] [sep] Azeotropic distillation column of Methanol / Isopropanol with Water by DeRosier.
[pdf] [sep] industrial i-butane/n-butane splitter as reported by Klemola and Ilme .
[pdf] [sep] How to model columns involving components that are not included in the databank.
[pdf] How to add compounds to the ChemSep databanks.
[fsd] Benzene/Toluene/p-Xylene separation train from ChemSep book.
[fsd] [png] DiMethylEther by dehydration of Methanol Dehydration of Methanol to produce DiMethylEther by Luyben in Ind.Eng.Chem.Res. (2010) Vol. 49 pp. 12224-12241.
[fsd] [png] Natural Gas Train Natural Gas separation train from Luyben in Ind.Eng.Chem.Res (2013) Vol. 52 pp. 10741-10753.
[fsd] [png] TAME Reactive distillation for producing Tert-Amyl Methyl Ether (TAME) from a cracked C5-cut by Luyben in Ind.Eng.Chem.Res. (2005) Vol. 44 pp. 5715-5725.
[fsd] [png] Methyl Acetate Esterification of Acetic Acid with Methanol to Methyl Acetate by means of reactive distillation as described in Reactive Distillation Design and Control by William L. Luyben and Cheng-Ching Yu, Wiley, NY (2006) pp. 147-164.
[fsd] [png] Light ends distillation Refinery light ends separations (depropanizer, debutanizer, deisobutanizer) by means of distillation by Luyben in Ind.Eng.Chem.Res., 52 (2013) pp. 15883-15895.
[fsd] [png] Methyl Acetate This case study is a modified version of the 1967 American Institute of Chemical Engineers student contest problem for the dealkylation of Toluene to Benzene with hydrogen, see "Conceptual Design of Chemical Processes", McGrawHill, 1988, or J.M Douglas, AIChE J., Vol. 31 (1985) p. 353. It features a gas phase reaction with gas recycle as well as a separation train with a recycle of unreacted toluene.
[fsd] [png] Light ends distillation EthylBenzene production from Ethylene and Benzene by Luyben in AIChE J. Vol. 57 (2011) pp. 655-670. Note that this flowsheet uses fixed conversion rates in the reactor whereas the original publication uses rate equations.
[fsd] [png] Methyl Ethyl Ketone Dehydrogenation of 2-Butanol to Methyl Ethyl Ketone catalyzed by In/MgO as per DE2831465A1 (1978)
[fsd] [png] Light ends distillation Hydration of Ethylene Oxide to Mono-Ethylene Glycol (MEG) using an uncatalyzed reactor at 200 C with kinetics from Ind.Eng.Chem.Res. 48 (2009) pp. 10840-10844.
[fsd] [png] Ethanol-Water Heterogeneous azeotropic distillation of Ethanol and Water, inspired by the flowsheet described by G. Prokopakis and W.D. Seider in AIChE J. 29 p. 49. This separation process model is extremely sensitive to small changes in the process specifications and also to the parameters used in the thermodynamic model.
[fsd] [png] C3MR - Propane Mixed Refrigerant Cycle for Natural Gas C3MR LNG Refrigeration Cycle for Natural Gas (NG). This flowsheet was inspired by that given in the report "Modelling and optimization of the C3MR process for liquefaction of natural gas," by Dag-Erik Helgestad (December 2009).
[fsd] [png] TEALARC TEALARC LNG Refrigeration Cycle for Natural Gas (NG). This flowsheet was based on one described in the report "Simulation, optimal operation and self optimisation of TEALARC LNG plant," by Emmanuel Orji Mba (December 2009).
[fsd] [png] Ethylene Cracker Ethylene Cracker with high purity separation train using UOP Multi-Downomer trays based on the debottlenecking of the EE splitter and the PP splitter of the Port Arthur (TX) Chevron Ethylene Cracker. "Stone and Webster's ARS technology was implemented in Chevron's ARS and refinery-gas dephlegmator coldboxes during the revamp in 1997. Chevron Chemical Co. LLC's Port Arthur, Tex., ethylene unit (EU-1544) was expanded from 1.0 billion lb/year to 1.7 billion lb/year.".
[fsd] [png] TEG NG Drying Drying of Natural Gas using TEG.
Perry Example 2 Perry Example 3 Perry Example 4 Perry Example 5 Perry Example 6 Examples from Chapter 13 Distillation of Perry's Chemical Engineers' Handbook:
2) Simple absorber for Butane and Pentane recovery from process gas using absorbent oil (here simulated with n-Dodecane),
3) Simple two cut splitter separating Butane and Pentane,
4) Three cut splitter with side-draw that creates a sloppy Butane cut,
5) Two-step absorber with internal cooling to maximize LPG recovery, and
6) Reboiled stripper to remove light gases (N2, C1-C3) from heavier compounds.
[fsd] [png] TEG NG Drying Ethanol Water separation with Benzene exhibiting multiplicity This example is one of the most famous in the entire literature on distillation column modeling having been studied, in one form or another, by many investigators including Magnussen et al. I.Chem.E.Symp.Series, 56 (1979), Prokopakis and Seider AIChE J., 29, 49 (1983), and Venkataraman and Lucia Comput.Chem.Engng., 12, 55 (1988). The column simulated here is adapted from the work of Prokopakis and Seider.
Liquid compositions for the multiple solutions.
[fsd] [png] Triple Column Pressure Swing Distillation Solvents recovery line-up based on Sep.Purif.Technol. 169 (2016) pp. 66-77 combining azeotropic distillation with pressure swing distillation into a three column line-up for recovery of Acrylonitril, Methanol, and Benzene. This mixture forms multiple azeotropes and its triangular diagram has several distillation boundaries at atmospheric pressure. The feasibility of the process was confirmed using rigorous steady-state simulations. This 3 column line-up is the most optimal column sequence in a global optimization to separate the azeotropic mixture.
[fsd] [png] Acetone from IsoPropanol Acetone is produced via several alternative processes, one of which is the Acetone Process via Dehydrogenation of 2-Propanol (IPA). This endothermic gas-phase reaction converts IPA to acetone and hydrogen. The process has two distillation columns and an absorber column in which a water stream is used to recover acetone. In Ind.Eng.Chem.Res. Vol. 50 pp. 1206-1218 (2011) Luyben showed that operating the absorber at an elevated pressure reduced Acetone losses but increases vent losses and raises the required temperature and cost of the vaporizer heat source. It also adversely affects the reaction kinetics because the reaction is non-equimolar and conversion decreases with increasing pressure. As such, a higher reactor temperature is required to achieve the desired conversion. The paper proposed the economically optimum design.
[fsd] [png] Energy Efficient Hybrid Separation The Energy Efficient Hybrid Separation process for Acetic Acid purification is based on Ind. Eng. Chem. Res. Vol. 45, pp. 8319-8328 (2006), a paper discussing strategies that combine one or more separation techniques with distillation where energy efficiency is studied using the novel concept of shortest separation lines. Such hybrid separation schemes include extraction followed by distillation, reactive distillation, adsorption/distillation, and others.
[fsd] [png] Hydrogenation of Benzene Cyclohexane can be produced by the Hydrogenation of Benzene by the ARCO Technology Inc. process as described in Hydrocarbon Processing, November (1977) p. 143. This process has been replaced by the more efficient and economic reactive distillation hydrogenation process from CDtech (US6187980).
[fsd] [png] Styrene from EthylBenzene The Styrene process from EthylBenzene is based on the Vasudevan design in Ind. Eng. Chem. Res. Vol. 48, pp. 10941 (2009), Figure 15.1. This paper discusses an improvement design over the Styrene plant in "Plant-Wide Process Control" by Luyben et al. (McGraw-Hill, NY, 1998).


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