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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.

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 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. If you are unfamiliar with COCO there are two introductions you can read to get started quickly: CAPE-OPEN Flowsheet Simulations with ChemSep and Flowsheeting with COCO and ChemSep (2010)

Files	Description
[fsd] [png]	NEW: Novel Hydrogren Liquefaction Cycle (26/3/2023) Novel hydrogen Liquefaction cycle as described by L. Yin and Y. Ju, Int. J.Refrig. 110 (2020) pp. 219-230, which utilizes a liquid nitrogen pre-cooling system as well as a helium cryogenic cycle. The regular Hydrogen component is normally simulated as a single molecule but in this cycle we distinguish between the ortho- and para-magnetic isomers Hydrogen actually consists of. Hence we first convert a stream consisting of regular Hydrogen component into the two isomers. At room temperature Hydrogen consists of 75 percent ortho-H2 and 25 percent para-H2. Then the conversion between the two isomers para-hydrogen and ortho-hydrogen is achieved in a series of reactors loaded with Iron (III) Hydroxide (Fe(OH)3) as the catalyst. The original publication did not account for the energy difference between ortho- and para-Hydrogen. This was corrected by inclusion of an offset for the Heat of Formation of ortho-H2. This is why the conversion of regular Hydrogen into its two isomers has a heat effect that in reality isn't there.
[fsd] [png]	Energy efficient process for CO2 removal from Natural Gas for CCS (14/2/2023) Park et al. (2021) (Energy, Vol 214, p. 118844) describe an energy efficient process for low temperature CO2 removal from natural gas using an R134a refrigeration cycle. This patented process, like the SPREX process, is limited to produce a methane-rich product with 20-25 mol% of CO2 concentration. To produce natural gas with sales specification, an additional CO2 removal unit will be required. The simulation here uses the Peng-Robinson Equation of State.
[fsd] [png]	Rectisol Process for SynGas with CO2 for EOR (15/1/2023) This process describes the Rectisol process to remove all CO2 from syn-gas by absorbing in cold methanol (Rectisol process) as described by Gatti et al. (2014). Note that some processes may benefit from not removing all CO2 from the syngas. The CO2 is compressed to a pressure of 150 bar for reservoir injection for Enhanced Oil Recovery purposes. The H2S removal is simplified and simulated as a simple Claus separation block.
[fsd] [png]	Extraction of Aromatics with Sulfolane (16/7/2022) from a refinery catalytic reformer stream after Figure 10.1 in T.Brouwer (PhD TU Twente 2021). Aromatics are removed from the stabilized reformate using a liquid-liquid extraction column with Sulfolane. The extractor is operated with a recycle of light C5 alkanes and Sulfolane is washed out from the raffinate with water. The aromatics are recovered from the sulfolane under vacuum conditions.
[fsd] [png]	Reformate Splitter (1/7/2022) of a refinery catalytic reformer using a Dividing Wall Column (DWC) after I. Dejanovic, L. Matijasevic, H. Jansen, Z. Olujic "Designing a Packed Dividing Wall Column for an Aromatics Processing Plant" Ind. Eng. Chem. Res. 50, pp. 5680-5692 (2011). Benzene is removed from the Mogas pool in this reformate splitter. Traditionally this is done with a side-stripper configuration producing a Benzene-rich heart-cut stream. This configuration is compared to a DWC with a sloped wall and to the Kaibel column that adds a Toluene-rich product. By performing multiple separations in a single shell the DWC requires less energy, less capital and less space than conventional columns-in-series and/or in-parallel configurations. As such DWC are an important tool for the petro- and petrochemicals process industry towards a more sustainable way of distilling products.
[fsd] [png]	Process for Fatty Acids (1/6/2022) from Palm Kernel Oil adapted from a Oleochemicals Chemicals 2011 presentation by OXITENO on their Brazilian process plants. This flowsheet demonstrates the use of multiple K-models. The SRK-UMR equation of state is used for the hydrolysis of the oil into fatty acids and the separation in C12, C14, C16, and C18 acids. Note that the C18 fatty acids are not lumped but split out over three fractions of Lineic, Linoleic, and Stearic acids. Consequently, the DECHEMA-UNIFAC model is used for the separation train of the fatty alcohols in vacuum columns. Some of the binary Vapor-Liquid diagrams of the fatty acids are displayed on the flowsheet. We use different colors to illustrate where each package is used: The units and streams using DECHEMA-UNIFAC are shown in green when solved.
[fsd] [png]	Process for Fatty Alcohols (1/6/2022) from Palm Kernel Oil adapted from a Oleochemicals Chemicals 2011 presentation by OXITENO on their Brazilian process plants. This flowsheet demonstrates the use of multiple K-models. The SRK-UMR equation of state is used for the hydrolysis of the oil into fatty acids, the conversion of these to Fatty Acids Methyl Esters (FAME) and the hydrogenation of FAME to the fatty alcohols. Consequently, the DECHEMA-UNIFAC model is used for the separation train of the fatty alcohols in vacuum columns. The binary Vapor-Liquid diagrams of the fatty acids are displayed on the flowsheet. Note we also use different color schemes to illustrate where each package is used. The units and streams using SRK-UMR display in dark grey when solved whereas those units and streams using DECHEMA-UNIFAC are shown in green when solved.
[fsd] [png]	Process for Isopropyl Alcohol (25/7/2021) synthesis from Propylene and Water adapted from Niu et al., Ind. Eng. Chem. Res. 2016, 55, 12, pp. 3614-3629. This flowsheet demonstrates the use of multiple K-models. The Peng-Robinson equation of state is used for the separation of propylene from propane allowing for the reactant to be recycle back to the reactor. The NRTL model is used for the remaining operations of the process and the binary interaction parameters have been fit to available experimental data for the nonideal binary mixtures involved in this process. Due to the possibility of three phases in the pairs containing Propane/Proylene and Water the UNIFAC model is used to predict those parameters. To increase temperature and prevent two liquid phases from forming, the first column utilizes a partial condenser. The most difficult separation in this process is between Water and Isopropyl Alcohol therefore the solvent DMSO (Dimethyl Sulfoxide) is introduced to the final separation section effectively allowing for a desirable final product of IPA. Niu et al. describe additional improvements that can made to this process.
[fsd] [png]	Ethanol-Amines process (15/7/2021). Process for a SRI 45 KTA Mono-Ethanol-Amine (MEA) / Di-Ethanol-Amine (DEA) / Tri-Ethanol-Amine (TEA) production as per US 4,355,181 and described in Korean J. Chem. Eng Vol. 26, No. 6 pp. 1504-1511 (2009), using fixed conversion reactors and a substitute for the heavier ethanol amines. Two different ChemSep Cape-Open Property Packages are used: The SRK-UMR is used to describe the VLE in the high pressure reactor section and the gamma-phi method with NRTL parameters predicted from UNIFAC is used for the vacuum distillation of the ethanolamines.
[fsd] [png]	Ethyl-Benzene Styrene Monomer process (4/4/2021). Combined Ethyl-Benzene (EB) Styrene Monomer (SM) process as shown in the 2005 AIChE Spring Meeting presentation "Design Guidelines for Distillation Columns in Ethyl-benzene and Styrene Monomer Service" by Peter Faessler et al. who discuss the Badger-SM process with details about revamping of the EB/SM splitter with high capacity structured packing for increasing performance specifciations. The flowsheet features the use of different ChemSep Cape-Open Property Packages (ChemSep/Copp) for the high and low pressure operations.
[fsd] [png]	Extraction separation of CO2 from NG (24/1/2021). For many years CO2 has been injected into oil and gas wells in an effort to extract more crude oil and natural gas. After methane has been separated from the CO2-rich gas in a demethanizer the CO2 needs to be recovered so that it can be re-injected into the well. The separation of CO2 from the ethane rich fluid is complicated because of an azeotrope that exists between CO2 and ethane. One approach to breaking azeotropes is via extractive distillation. In the process in this document the solvent is a mixture of the higher molecular weight hydrocarbons. This flowsheet was adapted from one described by W.L. Luyben. Ours uses the PPR78 EOS which employs a group contribution method for the estimation of temperature dependent binary interaction parameters. Luyben, W. L. Control of an Extractive Distillation System for the Separation of CO2 and Ethane in Enhanced Oil Recovery Processes Ind.Eng.Chem.Res. (2013) 52 pp. 10780-10787.
[fsd] [png]	This flowheet was inspired by the article of Dimian and Kiss on the Acetic Acid Cativa(TM) process (21/2/2021) for making acetic acid from carbon monoxide and methanol, see Chem.Eng.Res.Des. (2020) 159, pp. 1-12. The recycle is estimated; neither Dimian and Kiss nor we included the necessary recovery units in the model. This flowsheet examplifies the use of two different K-models: PSRK equation of state for the high pressure reactor section and gamma-phi model for the separation section where the difficult separation between acetic acid and water is key. The binary interaction parameters have been fit to data for most of the nonideal binary mixtures found in this process. There is scope for further improvement in modeling the solubility of the light gases in the separaton section; here we adopted the approach of Prausnitz et al. (1980).
[fsd] [png]	Improved BenzOut Process (29/12/2020) using a Dividing Wall Column (with sloped wall) with enhanced product recovery. This process was developed by ExxonMobile (CA2754816C) and features a zeolite fixed bed liquid reactor operating at low temperatures where the Benzene in reformate from a CCR is converted for 95% to alkylbenzenes by reacting it with refinery grade (95%) Propylene from a FCC unit. This generates a Mogas blending stream with a higher octane number (by 2-3 points on RON/MON) that is within Benzene specification. As a by-product Propane of HD5 quality is generated. By combining this process with the Dividing Wall Column (DWC) as disclosed by Dejanovic et al. as described in Ind. Eng. Chem. Res. (2011) Vol. 50 pp. 5680-5692 (with sloped wall DWC) an approximate 40% reduction in Total Annulized Cost and a 5% larger product flowrate can be obtained. The DWC produces a heart-cut Benzene rich stream that results in smaller reactors that can be run with a 99% conversion. The resulting stream is stabilized and mixed with the heavy reformate stream.
[fsd] [png]	Exergy and economic assessment of a solar-driven Kalina cycle (4/1/2021) with Ammonia-Water as per Mehrpooya and Mousavi in Energy Conversion and Management (2018) 178, pp. 78-91
[fsd] [fsd] [fsd] [fsd] [fsd] [fsd] [png]	Refrigeration cycles with Ammonia, Propylene, 2-step Propylene+Ethylene, 3-step Propylene+Ethylene+Methane, and 4-step Propylene+Ethylene+Methane+Nitrogen for cooling at -30, -50, -100, -150, and -190 C as described by Luyben (2019) in Chem.Eng.Process.Intens. 138 (2019) pp. 97-110 and Comp.Chem.Engng 126 (2019) pp. 241-248 (17/1/2021).
[fsd] [png]	Ethylene Oxide Process as per US 7,598,405 (18/1/2021) co-producing high purity Ethylene Oxide (EO) and Ethylene Glycol (EG). The reactor was setup around Start of Run (SOR) data on inlet and outlet mass rates provided in the 2015 PhD thesis by Samir C. Nimkar on the Exergy Analysis of industrial chemical processes. At SOR the reactor outlet temperature is 233 C. At 20.5 bar the high activity catalyst reaches an initial selectivity of 81% and 12.2% Ethylene conversion per pass. Conversion of undesired by-products Acetaldehyde and Formaldehyde were set to 0.1% and 0.01%, respectively (as per 2012 PhD thesis of Madhav Ghanta). The simulation here is setup for an EO production of just 1 t/h whereas real industrial reactors are sized to produce anywhere from 50 to 150 t/h.
[fsd] [png]	Alkylation of Butene and Isobutane (26/1/2021) as described by Luyben in Principles and Case Studies of Simultaneous Design (Wiley, 2011). This flowsheet implements a simplification of the Kellogg Sulfuric Acid Butene-Butane Alkylation Process, as adapted from figure 7.2 in Chapter 7. Reaction parameters from R. Mahajanam, R.V. Zheng, J.M. Douglas, "A shortcut method for control variable section and its application to the butane alkylation process", Ind. Eng. Chem. Res. (2001) 40, p. 3208. Note: To converge from a resetted flowsheet you need to hook-up both the gas and liquid recycle flows as given in Luyben. After convergence is obtained you can then link-up the liquid recycle first, and solve again. After converging the flowsheet again the gas recycle can also be linked-up.
[fsd] [png]	Carbonylation of Di-Methyl Ether with CO to Methyl Acetate (19/8/2020) by Diemer and Luyben in Ind.Chem.Eng.Res.Des. Vol. 49 page 12224-12241. Dimethyl ether (DME) is produced by dehydration of Methanol. In a second step DME is carbonylized with CO over zeolites to produce Methyl Acetate (for kinetics see Cheung et al. Angew.Chem.Int.Ed. (2006) 45, pp. 1617-1620 The process illustrates a number of important design trade-offs among the many design optimization variables: reactor temperatures, reactor pressures, distillation column pressures, reactor sizes and purge composition.
[fsd] [png]	Extractive Distillation of Di-Methyl Carbonate (DMC) and Methanol (6/4/2020) using four different solvents as described in Ind.Chem.Eng.Res.Des. Vol. 127 page 189. DMC forms an azeotrope with Methanol. The paper discusses a holistic, three-tiered approach to find alternative extractive distillation entrainers via a preliminary entrainer screening, measurement of limiting activity coefficients via headspace gas chromatography, and full binary Vapor-Liquid Equilibria measurements using a dynamic recirculation cell. The effectiveness of the entrainers were then quantitatively assessed by simulation of the heat-integrated line-ups and compared with that of the industrially used entrainer, Phenol. The simulation results reveal Methyl Salicylate as an MSA outperforms all other entrainers. This flowsheet illustrate how ChemSep can perform the fitting of the four new binary VLE data-sets to obtain UNIQUAC binary interaction parameters which are used in a ChemSep Cape-Open Property Package (CS/COPP) and how the sizing of the columns on the rating panel can directly provide the Total Annualized Cost (TAC) for each entrainer at the flowsheet level to optimize the process.
[fsd] [png] [MSH fsd] [MSH png]	Cold box for the production of Propylene by Propane DeHydrogenation (PDH) from US 6,333,445 from Chart, Inc (21/2/2020).
[fsd] [png]	LPG Divided Wall Column (19/5/2019) for a lower cost separation of LPG from Natural Gas as described in December 2018 Gas Processing issue.
[fsd] [fsd MSHX] [pdf] [png]	ASU (27/5/2018) flowsheet by H.Kooijman (original 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]	Process to synthesize Butyl Acetate from Methyl Acetate and Butanol (18/12/2011), 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]	Process for producing Cumene from Benzene and Propylene (18/12/2011) 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]	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]	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 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 as described by Luyben in Ind. Eng. Chem. Res. (2009) Vol. 48 pp. 6034-6049 simulated as one column.
[fsd] [png]	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]	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]	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]	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]	Dehydration of Methanol to produce DiMethylEther (DME) as described by Diemer and Luyben in Ind.Chem.Eng.Res.Des. Vol. 49 page 12224-12241.
[fsd] [png]	Natural Gas separation train from Luyben in Ind.Eng.Chem.Res (2013) Vol. 52 pp. 10741-10753.
[fsd] [png]	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]	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]	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]	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]	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]	Dehydrogenation of 2-Butanol to Methyl Ethyl Ketone catalyzed by In/MgO as per DE2831465A1 (1978)
[fsd] [png]	Hydration of Ethylene Oxide to Mono-Ethylene Glycol (MEG) (19/12/2013) using an uncatalyzed reactor at 200 C with kinetics from Ind.Eng.Chem.Res. 48 (2009) pp. 10840-10844.
[fsd] [png]	Heterogeneous azeotropic distillation of Ethanol and Water (23/2/2016) 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] [fsd] [png]	C3MR LNG Refrigeration Cycle for Natural Gas (14/1/2014). 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] [fsd] [png]	TEALARC LNG Refrigeration Cycle for Natural Gas (21/2/2016). 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 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]	Drying of Natural Gas using TEG.
[fsd][png] [fsd][png] [fsd][png] [fsd][png] [fsd][png]	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]	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. .
[fsd] [png]	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 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]	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]	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]	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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