aspen hysys v8 test case certification 21 jan 13-final

Confidential

This documentation contains AspenTech proprietary and confidential information and may not be disclosed, used or

copied without the prior consent of AspenTech.

Aspen HYSYS V8.0

Test-Case Certification

Confidential Test-Case Certification 2 Aspen HYSYS V8.0

Table of Contents

1 Introduction ........................................................................................................................................ 3

2 Test Procedure ................................................................................................................................... 3

3 Test Files Used for Certification ....................................................................................................... 4

4 Test File Comparison Results Summary ....................................................................................... 12

5 Test File Comparison Results Detail.............................................................................................. 14


1 Introduction

The Aspen HYSYS V8.0 Test-Case Certification documents the results of a series of tests that

compare the results generated by Aspen HYSYS V8.0 with those generated by Aspen HYSYS

V7. 3, both updated with the latest patches available on the AspenTech Support website.

We hope that this will help you in the process of upgrading to V8.0 by demonstrating that

results from V8.0 are generally consistent with those from V7.3. We will also explain the

reasons for any differences that were found during certification testing.

2 Test Procedure This certification from AspenTech is based on the approved process and a set of canned

test files.

The tests run 43 of the example files included with Aspen HYSYS V7.3. These files are a

subset of example cases delivered in HYSYS and encompass all major functional areas.

These examples run in both V7.3 and V8.0. The results for the temperature, pressure, flow

rate and mass composition of all streams are compared.

The tests were performed using the Aspen Version Comparison Assistant. This tool

automates the process of running the tests and comparing the stream results. The Aspen

Version Comparison Assistant works with Aspen HYSYS and Aspen Plus, and is available for

you to use with your test files


3 Test Files Used for Certification

Test File Name Description

Acid Gas Sweetening with DEA.hsc In this application a sour natural gas stream is stripped of H2S and CO2 in a Contactor (absorber) tower. The rich DEA (diethanolamine) is regenerated in a Stripping tower and the lean DEA is recycled back to the Contactor. To solve this example, the DBR Amine property package should be used.

Ammonia Synthesis.hsc This model has been set up to demonstrate OLE links, and the use of an external optimizer. The case can be used standalone, but it also works together with an Excel spreadsheet, from which the optimizer can be run using the Tools|Solver command.

AssayWithDifferentLightEndsBasis.hsc This model is to calculate light ends composition (molar basis) and TBP curves (mass basis) from input data on difference basis.

Atmospheric Crude Tower.hsc In this example 100,000 barrel/day of 29.32o API crude is fed into a pre-flash separator after passing through a preheat train. The vapor from this separator bypasses the crude furnace and is re-mixed with the hot pre-flash liquids leaving the furnace. The combined stream is then fed to the atmospheric crude column. The column operates with a total condenser, three coupled side strippers, and three pump around circuits.

Biodiesel Alkali Process.hsc This example models an alkali-catalyzed process for the transesterification process in commercial biodiesel production.


Biodiesel process_3 phase separation.HSC This model provides an example of liquid product separation from a biodiesel production process.

BlackOilStreamBulkProperties.hsc This example models Oil and Gas feed stream when only bulk properties such as GOR, WOR, Std. Liquid Density and Watson K are provided.

BlackOilStreamWithPetroleumProperties.hsc This example models Oil and Gas feed stream when a library petroleum assay is being used.

ClausProcess.hsc The Claus process is widely used to recover sulfur from acid gases that contain hydrogen sulfide. This example models a Claus process using reactors and component splitters.

Crude Oil Fractionation Facility.hsc In this application, crude oil is processed in a fractionation facility to produce naphtha, kerosene, diesel, atmospheric gas oil, and atmospheric residue products.

Crude_Preheat_Train_with_Fired_Heater.hsc This model is to demonstrate how to evaluate the potential energy savings for a crude preheat train. The starting point is any feasible alternative to integrate a crude preheat train. It starts in the analysis of the maximum thermodynamically possible energy savings for the set of process streams under consideration.

Deep Cut Turbo-Expander Plant.hsc In this example, a natural gas stream containing N2, CO2, and C1 through n-C4 is processed in a refrigeration system to remove the heavier hydrocarbons. A turbo expander and propane refrigeration unit are modeled to achieve deep cut extraction.

Depressuring Example.hsc The purpose of this model is to compare the dynamic depressuring utility against a reference case listed below. M.A. Haque, S.M. Richardson, G. Saville, G.


Chamberlain and L.Shirvill, Blowdown of Pressure Vessels - II. Experimental Validation of Computer Model and Case Studies, Institution of Chemical Engineers, Trans IChemE, Vol 70, Part B, February 1992.

Ethanol Dehydration.hsc This model demonstrates how to model separation sequences for ethanol dehydration using benzene.

Ethanol Plant.hsc An ethanol production process is modeled right from the fermentor outlet to the production of low grade and high grade (azeotropic) ethanol products.

FCC And Gas Plant.hsc This example is a model of a process for a FCC (Fluid Catalytic Cracking) unit; a FCC main fractionator and a gas plant with absorber oil and heat integration recycle streams. It is intended to demonstrate on how to model the FCC reactor, how to model the FCC main fractionator and gas plant columns, and how to model the recycle loops.

Hydraulics-SS-1.hsc This is an example of how flow networks in an Aspen Hydraulics subflowsheet can be connected to the main HYSYS flowsheet. In this example, three streams with different phases on the main HYSYS flowsheet are mixed in an Aspen Hydraulics subflowsheet into a single stream. There are additional source streams defined in the Aspen Hydraulics subflowsheet.

Hydraulics-SS-2.hsc This is another example of how flow networks in an Aspen Hydraulics subflowsheet can be connected to the main HYSYS flowsheet. In this example, three streams with different phases on the main HYSYS flowsheet are mixed in an Aspen Hydraulics subflowsheet into a single stream. There are additional source streams defined in the Aspen Hydraulics subflowsheet.


Hydraulics-SS-3.hsc This is an example of flow network systems where a single stream splits into three streams with different outlet pressure specifications. The pressure specification on “Sink-1” results in a reverse flow at that boundary. The cases differ by the mass flow specification on the “Source” stream.

Hydraulics-SS-4.hsc This is second example of flow network systems where a single stream splits into three streams with different outlet pressure specifications. The pressure specification on “Sink-1” results in a reverse flow at that boundary. The cases differ by the mass flow specification on the “Source” stream.

HydrocrackerProductTransition.hsc This case demonstrates modeling a hydrocracker and using the standard hydrocracker product transition to get the HPS liquid on an assay basis. The kinetic lumps used by the hydrocracker have some large gaps between the boiling points of components, so the petroleum transition is not adequate for transitioning between the hydrocracker components and the assay components. The standard hydrocracker product transition maps from the hydrocracker component basis to the assay components in a smooth way so that the product is suitable for fractionation.

Hydrotreater model (short-cut).hsc This application models a diesel hydrotreater using the petroleum shift reactor.

LNG Plant Simulation.hsc This example provides a model for the LNG (Liquefied Natural Gas) process. It demonstrates on how to model the different sections of LNG process, and supplies a starting set of components and physical property parameters for modeling processes of this type.


Mixer.hsc This is a steady-state example of a mixer unit operation that combines two vapor phase streams in an Aspen Hydraulics subflowsheet.

Mixer – Two Phase.hsc This is a steady-state example of a mixer unit operation that combines two multiphase (vapor and liquid) streams in an Aspen Hydraulics subflowsheet.

MultipleFluidPackageHF.hsc This application models a Depropanizer such as that used in an alkylation unit in a refinery. The depropanizer uses a different basis for the condenser, to allow for the correct HF/Water split from the hydrocarbon.

Naphtha Complex.HSC This example models naphtha upgrading in a refinery. Straight-run and import naphthas are used and the flowsheet contains rigorous reformer and isomer units. Manipulators are used to set the correct PNA values and to remove sulfur.

Natural Gas Dehydration with TEG.hsc This example is meant to provide a starting point for advanced simulation of natural gas dehydration using TEG (Triethylene Glycol). It presenting a set of components with their physical properties, and the TEG regenerator and the TEG contactor modules with their specific interconnections.

Petroleum Column.HSC This application models petroleum distillation columns in a refinery. The Petroleum Column is specifically designed to help with solving the following problems: • Simulating a petroleum column for a wide range of crude oils within an optimization or gradient generation scenario. In these situations, the column needs to be simulated over and over again, and the column should converge quickly and consistently in all scenarios. • Manually calibrating the Petroleum Column


from plant data.

Pipeline Network1.hsc This is an example of gas pipeline network solution for a specified outlet pressure. The Equation Oriented formulation frees the inlet pressures, and therefore calculates the pressures to meet the flow and outlet pressure specifications.

Propylene Glycol Production Process.hsc This model demonstrates the production of propylene glycol by hydration of propylene oxide inside a CSTR (Continuous Stirred-Tank Reactor).

Propylene Glycol Production-2.hsc This is another model of the production of propylene glycol by hydration of propylene oxide inside a CSTR (Continuous Stirred-Tank Reactor).

Propylene-Propane Splitter.hsc This model includes the individual Stripper tower and Rectifier tower components of a propane/propylene splitter system. Two separate towers in the same column sub-flowsheet are used to illustrate the simultaneous solution power of Aspen HYSYS's Column sub-flowsheet.

Refinery-wide model.hsc This example illustrates using Petroleum Shift Reactors (short-cut models for refinery reactors) to build a refinery-wide flowsheet. It demonstrates how one could use a refinery-wide model to track materials (e.g. hydrogen) and utilities (e.g. steam, fuel,). It also shows how one could formulate the overall profit function on a spreadsheet and study refinery performance by manipulating the model degrees of freedom such as FCC conversion and reformer severity.


Single Pipe steady .hsc This is a steady-state example of multiphase (vapor and liquid) flow through a single pipe in an Aspen Hydraulics subflowsheet.

Single pipe.hsc This application models a single vapor phase flowing through a single pipe in an Aspen Hydraulics subflowsheet.

Single Pipe – Two Phase.hsc This model demonstrates multiphase (vapor and liquid) flow through a single pipe in an Aspen Hydraulics subflowsheet.

Single Valve.hsc This is a steady-state example of multiphase (vapor and liquid) flow through a valve in an Aspen Hydraulics subflowsheet.

Sour Water Stripper.hsc In this model sour water is fed to a distillation tower for NH3 and H2S removal. The use of the Sour Peng Robinson (Sour_PR) is highlighted. Aspen HYSYS's built-in Case Study tool is used to examine the effects of varying column feed temperatures.

Sweet Gas Refrigeration Plant.hsc In this example, a natural gas stream containing N2, CO2, and C1 through n-C4 is processed in a refrigeration system to remove the heavier hydrocarbons. The lean, dry gas produced will meet a pipeline hydrocarbon dew point specification. The liquids removed from the rich gas are processed in a depropanizer column, yielding a liquid product with specified propane content.

Synthesis Gas Production.hsc Synthesis gas (H2/N2 on a 3:1 basis) is the necessary feedstock for an ammonia plant. This model explores the traditional process for creating synthesis gas.

Tee.hsc This example models a tee unit operation that splits a vapor phase stream into two separate streams in an Aspen Hydraulics subflowsheet.


Tee – Two Phase.hsc This is a steady-state example of a tee unit operation that splits a multiphase (vapor and liquid) stream into two separate streams in an Aspen Hydraulics subflowsheet.


4 Test File Comparison Results Summary

Aspen HYSYS versions V7.3 and V8.0

Report Date: 21-Jan-13

Tolerances: Temperature 0.1 C

Pressure 0.1 %

Total Flow 0.1 %

Stream Composition 0.001

Model/File Date V7.3 Run V7.3 Status Date V8.0 Run V8.0 Status Differences

Acid Gas Sweetening with DEA.hsc 21-Jan-13 7:10 PM Simulation Successful 21-Jan-13 7:11 PM Simulation Successful 0

Ammonia Synthesis.hsc 21-Jan-13 7:11 PM Simulation Successful 21-Jan-13 7:12 PM Simulation Successful 0

AssayWithDifferentLightEndsBasis.hsc 21-Jan-13 7:12 PM Simulation Successful 21-Jan-13 7:12 PM Simulation Successful 0

Atmospheric Crude Tower.hsc 21-Jan-13 7:13 PM Simulation Successful 21-Jan-13 7:13 PM Simulation Successful 0

Biodiesel Alkali Process.hsc 21-Jan-13 7:13 PM Simulation Successful 21-Jan-13 7:14 PM Simulation Successful 0

Biodiesel process_3 phase separation.HSC 21-Jan-13 7:14 PM Simulation Successful 21-Jan-13 7:14 PM Simulation Successful 0

BlackOilStreamBulkProperties.hsc 21-Jan-13 7:14 PM Simulation Successful 21-Jan-13 7:15 PM Simulation Successful 0

BlackOilStreamWithPetroleumProperties.hsc 21-Jan-13 7:15 PM Simulation Successful 21-Jan-13 7:15 PM Simulation Successful 37

ClausProcess.hsc 21-Jan-13 7:16 PM Simulation Successful 21-Jan-13 7:16 PM Simulation Successful 0

Crude Oil Fractionation Facility.hsc 21-Jan-13 7:17 PM Simulation Successful 21-Jan-13 7:17 PM Simulation Successful 0

Crude_Preheat_Train_with_Fired_Heater.hsc 21-Jan-13 7:17 PM Simulation Successful 21-Jan-13 7:18 PM Simulation Successful 0

Deep Cut Turbo-Expander Plant.hsc 21-Jan-13 7:18 PM Simulation Successful 21-Jan-13 7:18 PM Simulation Successful 0

Depressuring Example.hsc 21-Jan-13 7:18 PM Simulation Successful 21-Jan-13 7:19 PM Simulation Successful 0

Ethanol Dehydration.hsc 21-Jan-13 7:19 PM Simulation Successful 21-Jan-13 7:19 PM Simulation Successful 0

Ethanol Plant.hsc 21-Jan-13 7:19 PM Simulation Successful 21-Jan-13 7:20 PM Simulation Successful 0

FCC And Gas Plant.hsc 21-Jan-13 7:21 PM Simulation Successful 21-Jan-13 7:25 PM Simulation Successful 0

Hydraulics-SS-1.hsc 21-Jan-13 7:30 PM Simulation Successful 21-Jan-13 7:31 PM Simulation Successful 0






HydrocrackerProductTransition.hsc 21-Jan-13 7:33 PM Simulation Successful 21-Jan-13 7:36 PM Simulation Successful 40

Hydrotreater model (short-cut).hsc 21-Jan-13 7:37 PM Simulation Successful 21-Jan-13 7:37 PM Simulation Successful 0

LNG Plant Simulation.hsc 21-Jan-13 7:37 PM Simulation Successful 21-Jan-13 7:37 PM Simulation Successful 0

mixer - Two Phase.hsc 21-Jan-13 7:38 PM Simulation Successful 21-Jan-13 7:38 PM Simulation Successful 0

mixer.hsc 21-Jan-13 7:38 PM Simulation Successful 21-Jan-13 7:39 PM Simulation Successful 0

MultipleFluidPackageHF.hsc 21-Jan-13 7:39 PM Simulation Successful 21-Jan-13 7:39 PM Simulation Successful 0

Naphtha Complex.HSC 21-Jan-13 7:41 PM Simulation Successful 21-Jan-13 7:46 PM Simulation Successful 217

Natural Gas Dehydration with TEG.hsc 21-Jan-13 7:46 PM Simulation Successful 21-Jan-13 7:46 PM Simulation Successful 0

Petroleum Column.HSC 21-Jan-13 7:47 PM Simulation Successful 21-Jan-13 7:47 PM Simulation Successful 0

Pipeline Network1.hsc 21-Jan-13 7:48 PM Simulation Successful 21-Jan-13 7:49 PM Simulation Successful 0

Propylene Glycol Production Process.hsc 21-Jan-13 7:49 PM Simulation Successful 21-Jan-13 7:49 PM Simulation Successful 0

Propylene Glycol Production-2.hsc 21-Jan-13 7:50 PM Simulation Successful 21-Jan-13 7:50 PM Simulation Successful 0

Propylene-Propane Splitter.hsc 21-Jan-13 7:50 PM Simulation Successful 21-Jan-13 7:51 PM Simulation Successful 0

Refinery-wide model.hsc 21-Jan-13 7:52 PM Simulation Successful 21-Jan-13 7:54 PM Simulation Successful 0

single Pipe - Two Phase.hsc 21-Jan-13 7:57 PM Simulation Successful 21-Jan-13 7:57 PM Simulation Successful 0

single Pipe steady .hsc 21-Jan-13 7:58 PM Simulation Successful 21-Jan-13 7:58 PM Simulation Successful 0

single pipe.hsc 21-Jan-13 7:58 PM Simulation Successful 21-Jan-13 7:59 PM Simulation Successful 0

single Valve.hsc 21-Jan-13 7:59 PM Simulation Successful 21-Jan-13 7:59 PM Simulation Successful 0

Sour Water Stripper.hsc 21-Jan-13 7:59 PM Simulation Successful 21-Jan-13 8:00 PM Simulation Successful 0

Sweet Gas Refrigeration Plant.hsc 21-Jan-13 8:00 PM Simulation Successful 21-Jan-13 8:00 PM Simulation Successful 0

Synthesis Gas Production.hsc 21-Jan-13 8:00 PM Simulation Successful 21-Jan-13 8:01 PM Simulation Successful 0

Tee - Two Phase.hsc 21-Jan-13 8:01 PM Simulation Successful 21-Jan-13 8:01 PM Simulation Successful 0

Tee.hsc 21-Jan-13 8:01 PM Simulation Successful 21-Jan-13 8:02 PM Simulation Successful 0



BlackOilStreamWithPetroleumProperties.hsc 21-Jan-13 7:15 PM Simulation Successful 21-Jan-13 7:15 PM

Simulation Successful 37

Stream Variables V7.3 V8.0 Unit Difference Above Tolerance

MyBlackOilStream Flow 302392 445147 kg/h 47.208516% Yes

MyBlackOilStream Composition.C11* 0.0405891 0.0434569

0.0028678 Yes


0.00195696 Yes


0.00279389 Yes


0.00364112 Yes


0.0041148 Yes


0.00329632 Yes


0.00321503 Yes


0.00231612 Yes


0.00230788 Yes


0.00270208 Yes


0.00374973 Yes


0.00216955 Yes


0.00537575 Yes


0.00103565 Yes


0.00150857 Yes


0.00133233 Yes


0.00102303 Yes


0.00118021 Yes

5 Test File Comparison Results Detail




0.00117009 Yes


0.00150288 Yes


0.00121409 Yes


0.00108771 Yes


0.00146674 Yes


0.00160052 Yes


0.00195074 Yes


0.0023293 Yes


0.0032289 Yes


0.00322961 Yes


0.00850828 Yes


0.00393804 Yes

MyBlackOilStream Composition.Ethane 0.00476511 0.00320302

0.00156209 Yes

MyBlackOilStream Composition.H2O 0.00994862 0.000959475

0.00898914 Yes

MyBlackOilStream Composition.i-Butane 0.00454442 0.00309566

0.00144877 Yes

MyBlackOilStream Composition.Methane 0.119647 0.0803171

0.0393299 Yes

MyBlackOilStream Composition.n-Butane 0.00450456 0.00309566

0.0014089 Yes

MyBlackOilStream Composition.Propane 0.00347788 0.00234858

0.0011293 Yes

Comment: The differences found are due to an update to the example case file. In V7.3, the compositions of feed

streams to separators were specified while these should have been calculated based on the petroleum assay

supplied. In V8.0 such specified values are removed and the change leads to different results.



HydrocrackerProductTransition.hsc 21-Jan-13 7:33 PM Simulation Successful 21-Jan-13 7:36 PM



PRODUCT Composition.100-110* 0.0199205 0.0214481

0.00152757 Yes


0.00795125 Yes


0.00250557 Yes


0.00291434 Yes


0.0265278 Yes


0.00340607 Yes


0.00400141 Yes


0.00454695 Yes


0.00546724 Yes


0.00639925 Yes


0.00256763 Yes


0.00245612 Yes


0.00223999 Yes


0.00123909 Yes


0.00266391 Yes


0.00221014 Yes


0.00109407 Yes


0.00352114 Yes


0.00273809 Yes


0.00103328 Yes


0.00307917 Yes


0.00417908 Yes


0.0178783 Yes


0.025632 Yes




0.0184251 Yes


0.0151354 Yes


0.0117696 Yes


0.0079141 Yes


0.00438031 Yes


0.00232446 Yes


0.0145755 Yes


0.0373689 Yes


0.0295232 Yes


0.0299694 Yes


0.0150249 Yes


0.00512239 Yes


0.00325158 Yes


0.00185126 Yes


0.00140539 Yes

PRODUCT Composition.700+* 0.000374877 0.0105855

0.0102106 Yes

Comment: The differences are due to changes in HBED model (as explained in case “FCC_w_Hydrotreater.hsc”),

hydrocracker model and hydrocracker product transition that affect the results. The first change correctly sets

the light end basis to mass in V8.0 and the second sets up the mapping factors and cut points to correspond to

what is reported on the yields page of the hydrocracker.



Naphtha Complex.HSC 21-Jan-13 7:41 PM Simulation Successful 21-Jan-13 7:46 PM



Isom Unit.BEN Flow 0.163047 0.186223 kg/h 14.214516% Yes

Isom Unit.C7+ Flow 1311.46 1299.77 kg/h 0.891610% Yes

Isom Unit.Cold Feed Temperature 16.0464 16.3274 C 0.281023 Yes

Isom Unit.Hypos Composition.A6 0.00630325 0.00973526

0.003432 Yes

Isom Unit.Hypos Composition.NP7 0.978607 0.974675

0.00393178 Yes

Isom Unit.IC4 Flow 350.653 349.77 kg/h 0.251741% Yes

Isom Unit.IC6 Flow 13190.2 13229 kg/h 0.294675% Yes

Isom Unit.IC6 Composition.5N6 0.0944841 0.0955358

0.00105166 Yes

Isom Unit.Isom Hydrogen Feed Flow 526.005 520.903 kg/h 0.969952% Yes

Isom Unit.Isom Hydrogen Feed Composition.A6 0.0193708 0.0270697

0.00769896 Yes

Isom Unit.Isom Hydrogen Feed Composition.H2 0.630102 0.618283

0.0118198 Yes

Isom Unit.Isom Hydrogen Feed Composition.NP6 0.0189334 0.0228907

0.00395733 Yes

Isom Unit.Isom Off Gas Flow 2334.67 2301.34 kg/h 1.427463% Yes

Isom Unit.Isom Off Gas Composition.H2 0.0861714 0.0832742

0.00289718 Yes

Isom Unit.Isom Off Gas Composition.IP4 0.278199 0.281056

0.00285693 Yes

Isom Unit.Isom Off Gas Composition.IP5 0.0724489 0.0699166

0.00253224 Yes

Isom Unit.Isom Off Gas Composition.NP4 0.111839 0.113133

0.00129331 Yes

Isom Unit.Isom Off Gas Composition.P3 0.330293 0.33352

0.0032273 Yes

Isom Unit.Isomerate Temperature 53.3227 53.4401 C 0.117474 Yes

Isom Unit.Isomerate Flow 27383.3 27414.3 kg/h 0.113205% Yes

Isom Unit.Isomerate- Temperature 53.3227 53.4401 C 0.117474 Yes

Isom Unit.Isomerate- Flow 27383.3 27414.3 kg/h 0.113205% Yes

Isom Unit.Isomerate ISOM1 Temperature 193.601 192.652 C 0.948961 Yes

Isom Unit.Isomerate pre-RON fit Temperature 53.3227 53.4401 C 0.117474 Yes



Isom Unit.Isomerate pre-RON fit Flow 27383.3 27414.3 kg/h 0.113205% Yes

Isom Unit.Isomerate to Stab heater Flow 32392.5 32424.9 kg/h 0.100203% Yes

Isom Unit.Isomerate to Storage Flow 3389.02 3415.73 kg/h 0.788115% Yes

Isom Unit.NC4 Flow 364.298 362.827 kg/h 0.403813% Yes



Isom Unit.Other Flow 740.388 741.198 kg/h 0.109400% Yes

Isom Unit.ProdSep Off-gas- Flow 724.083 688.076 kg/h 4.972770% Yes

Isom Unit.ProdSep Off-gas- Composition.P1 0.041537 0.0426398

0.00110274 Yes

Isom Unit.Stabilizer Feed Flow 32392.5 32424.9 kg/h 0.100203% Yes

Isom Unit.Stabilizer Off-gas-- Flow 1610.58 1613.26 kg/h 0.166430% Yes

T-100.My SubFlowsheet.6301E Feed Flow 47833.5 48182 kg/h 0.728593% Yes

T-100.My SubFlowsheet.6301E Feed Composition.110-120* 0.1723 0.16777

0.00453041 Yes


0.00367718 Yes


0.002677 Yes


0.00273119 Yes

T-100.My SubFlowsheet.6301E Feed Composition.Benzene 0.00945463 0.0134915

0.0040369 Yes

T-100.My SubFlowsheet.6301E Feed Composition.n-Hexane 0.0064345 0.00791774

0.00148324 Yes

T-100.My SubFlowsheet.6320F Liquid Temperature 213.673 212.925 C 0.748467 Yes

T-100.My SubFlowsheet.6320F Liquid Flow 6494.25 6826.15 kg/h 5.110715% Yes

T-100.My SubFlowsheet.6320F Liquid Composition.110-120* 0.279101 0.267806

0.0112949 Yes


0.00143116 Yes


0.00295805 Yes


0.0127336 Yes

T-100.My SubFlowsheet.6320F Liquid Composition.Benzene 0.0537501 0.0749863

0.0212362 Yes

T-100.My SubFlowsheet.6320F Liquid Composition.n-Hexane 0.0435521 0.0516952

0.00814308 Yes

T-100.My SubFlowsheet.6320F Off Gas Temperature 213.673 212.925 C 0.748467 Yes

T-100.My SubFlowsheet.6320F Off Gas Flow 279.954 280.796 kg/h 0.300811% Yes



T-100.My SubFlowsheet.6320F Off Gas Composition.110-120* 0.216835 0.205289

0.0115455 Yes


0.00137118 Yes

T-100.My SubFlowsheet.6320F Off Gas Composition.2-Mpentane 0.0211039 0.0221343

0.0010304 Yes


0.00188378 Yes


0.00366826 Yes


0.0149946 Yes

T-100.My SubFlowsheet.6320F Off Gas Composition.Benzene 0.0652751 0.0901051

0.0248301 Yes

T-100.My SubFlowsheet.6320F Off Gas Composition.n-Hexane 0.0594773 0.0700302

0.0105529 Yes

T-100.My SubFlowsheet.Boilup Temperature 295.806 296.255 C 0.448586 Yes

T-100.My SubFlowsheet.Boilup Flow 71933.6 73423.6 kg/h 2.071427% Yes

T-100.My SubFlowsheet.Boilup Composition.110-120* 0.211199 0.205874

0.00532498 Yes


0.00689742 Yes


0.00203279 Yes


0.00132237 Yes


0.00418037 Yes

T-100.My SubFlowsheet.Boilup Composition.Benzene 0.00378138 0.00503467

0.00125329 Yes

T-100.My SubFlowsheet.Platformate Temperature 295.806 296.255 C 0.448586 Yes

T-100.My SubFlowsheet.Platformate Composition.110-120* 0.155104 0.150888

0.00421559 Yes


0.00563284 Yes


0.00173154 Yes


0.00199894 Yes


0.00259456 Yes

T-100.My SubFlowsheet.Reflux Temperature 213.673 212.925 C 0.748467 Yes

T-100.My SubFlowsheet.Reflux Flow 10246.2 10744.2 kg/h 4.860615% Yes

T-100.My SubFlowsheet.Reflux Composition.110-120* 0.279101 0.267806

0.0112949 Yes


0.00143116 Yes


0.00295805 Yes




0.0127336 Yes

T-100.My SubFlowsheet.Reflux Composition.Benzene 0.0537501 0.0749863

0.0212362 Yes

T-100.My SubFlowsheet.Reflux Composition.n-Hexane 0.0435521 0.0516952

0.00814308 Yes

T-100.My SubFlowsheet.To Condenser Temperature 241.443 240.459 C 0.98395 Yes

T-100.My SubFlowsheet.To Condenser Flow 17020.4 17851.2 kg/h 4.881042% Yes

T-100.My SubFlowsheet.To Condenser Composition.110-120* 0.278077 0.266823

0.0112541 Yes


0.00144099 Yes


0.0029717 Yes


0.0127655 Yes

T-100.My SubFlowsheet.To Condenser Composition.Benzene 0.0539397 0.0752241

0.0212844 Yes

T-100.My SubFlowsheet.To Condenser Composition.n-Hexane 0.0438141 0.0519836

0.00816955 Yes

T-100.My SubFlowsheet.To Reboiler Temperature 289.328 289.808 C 0.479833 Yes

T-100.My SubFlowsheet.To Reboiler Flow 112993 114499 kg/h 1.332666% Yes

T-100.My SubFlowsheet.To Reboiler Composition.110-120* 0.190815 0.186149

0.00466665 Yes


0.00651732 Yes


0.00192389 Yes


0.0016433 Yes


0.0034871 Yes

T-100.My SubFlowsheet.To Reboiler Composition.Benzene 0.00315875 0.00421441

0.00105566 Yes

C3+C4 Flow 8850.87 9160.82 kg/h 3.501920% Yes

C3+C4 Composition.110-120* 0.211646 0.205847

0.00579922 Yes

C3+C4 Composition.80-90* 0.0415564 0.0398011

0.00175536 Yes

C3+C4 Composition.90-100* 0.209313 0.202223

0.00708932 Yes

C3+C4 Composition.Benzene 0.0415034 0.0586377

0.0171343 Yes

C3+C4 Composition.i-Butane 0.0778762 0.0750374

0.00283878 Yes

C3+C4 Composition.i-Pentane 0.0313679 0.0296649

0.00170296 Yes

C3+C4 Composition.n-Butane 0.0483332 0.0467865

0.00154665 Yes

C3+C4 Composition.n-Hexane 0.034602 0.0413684

0.00676637 Yes



C3+C4 Composition.Propane 0.0908396 0.0874605

0.00337908 Yes

Gasoline Product Temperature 166.548 166.754 C 0.206535 Yes

Gasoline Product Composition.110-120* 0.0930478 0.0904918

0.00255603 Yes


0.00332612 Yes


0.00102112 Yes


0.00122699 Yes


0.00162916 Yes

Isom Hydrogen Feed Composition.110-120* 0.0960638 0.0926777

0.00338612 Yes

Isom Hydrogen Feed Composition.90-100* 0.0725096 0.0691527

0.00335681 Yes

Isom Hydrogen Feed Composition.Benzene 0.0133051 0.0187839

0.00547877 Yes

Isom Hydrogen Feed Composition.Hydrogen 0.432842 0.429077

0.00376522 Yes

Isom Hydrogen Feed Composition.n-Hexane 0.0130054 0.0158849

0.0028795 Yes

Isom Off Gas Flow 2332.51 2299.31 kg/h 1.423185% Yes

Isom Off Gas Composition.Hydrogen 0.0862561 0.0833525

0.00290365 Yes

Isom Off Gas Composition.i-Butane 0.278459 0.281306

0.00284738 Yes

Isom Off Gas Composition.i-Pentane 0.0725165 0.0699789

0.00253764 Yes

Isom Off Gas Composition.n-Butane 0.111944 0.113234

0.00128961 Yes

Isom Off Gas Composition.Propane 0.330601 0.333817

0.00321583 Yes

Isomerate Temperature 53.3227 53.4401 C 0.117474 Yes

Isomerate Flow 27383.5 27414.5 kg/h 0.113204% Yes

Light Ends Temperature 129.22 130.818 C 1.59851 Yes

Light Ends Flow 9195.93 9495.48 kg/h 3.257407% Yes

Light Ends Composition.110-120* 0.203705 0.198592

0.00511246 Yes


0.00159878 Yes


0.00636241 Yes

Light Ends Composition.Benzene 0.0399461 0.0565711

0.016625 Yes

Light Ends Composition.Hydrogen 0.0220342 0.0203356

0.00169861 Yes

Light Ends Composition.i-Butane 0.0749541 0.0723928

0.00256124 Yes



Light Ends Composition.i-Pentane 0.0301909 0.0286194

0.00157145 Yes

Light Ends Composition.n-Butane 0.0465196 0.0451376

0.00138198 Yes

Light Ends Composition.n-Hexane 0.0333036 0.0399104

0.00660676 Yes

Light Ends Composition.Propane 0.087431 0.0843781

0.00305295 Yes

Net Hydrogen Flow 4544.84 4657.56 kg/h 2.480326% Yes

Net Hydrogen Composition.110-120* 0.0960638 0.0926767

0.00338708 Yes

Net Hydrogen Composition.90-100* 0.0725096 0.0691522

0.00335735 Yes

Net Hydrogen Composition.Benzene 0.0133051 0.0187839

0.00547876 Yes

Net Hydrogen Composition.Hydrogen 0.432842 0.429074

0.00376784 Yes

Net Hydrogen Composition.n-Hexane 0.0130054 0.0158849

0.00287947 Yes

Net Hydrogen Product Flow 4173.24 4285.96 kg/h 2.701183% Yes

Net Hydrogen Product Composition.110-120* 0.0960638 0.0926767

0.00338708 Yes

Net Hydrogen Product Composition.90-100* 0.0725096 0.0691522

0.00335735 Yes

Net Hydrogen Product Composition.Benzene 0.0133051 0.0187839

0.00547876 Yes

Net Hydrogen Product Composition.Hydrogen 0.432842 0.429074

0.00376784 Yes

Net Hydrogen Product Composition.n-Hexane 0.0130054 0.0158849

0.00287947 Yes

Platformate Temperature 295.806 296.255 C 0.448586 Yes

Platformate Composition.110-120* 0.155104 0.150888

0.00421559 Yes


0.00563284 Yes


0.00173154 Yes


0.00199894 Yes


0.00259456 Yes

T-100 Feed Flow 47833.5 48182 kg/h 0.728593% Yes

T-100 Feed Composition.110-120* 0.1723 0.16777

0.00453041 Yes


0.00367718 Yes


0.002677 Yes


0.00273119 Yes

T-100 Feed Composition.Benzene 0.00945463 0.0134915

0.0040369 Yes



T-100 Feed Composition.n-Hexane 0.0064345 0.00791774

0.00148324 Yes

T-100 Liquid Temperature 213.673 212.925 C 0.748467 Yes

T-100 Liquid Flow 6494.25 6826.15 kg/h 5.110715% Yes

T-100 Liquid Composition.110-120* 0.279101 0.267806

0.0112949 Yes


0.00143116 Yes


0.00295805 Yes


0.0127336 Yes

T-100 Liquid Composition.Benzene 0.0537501 0.0749863

0.0212362 Yes

T-100 Liquid Composition.n-Hexane 0.0435521 0.0516952

0.00814308 Yes

T-100 Off Gas Temperature 213.673 212.925 C 0.748467 Yes

T-100 Off Gas Flow 279.954 280.796 kg/h 0.300811% Yes

T-100 Off Gas Composition.110-120* 0.216835 0.205289

0.0115455 Yes


0.00137118 Yes

T-100 Off Gas Composition.2-Mpentane 0.0211039 0.0221343

0.0010304 Yes


0.00188378 Yes


0.00366826 Yes


0.0149946 Yes

T-100 Off Gas Composition.Benzene 0.0652751 0.0901051

0.0248301 Yes

T-100 Off Gas Composition.n-Hexane 0.0594773 0.0700302

0.0105529 Yes

To Isom Composition.110-120* 0.0960638 0.0926767

0.00338708 Yes

To Isom Composition.90-100* 0.0725096 0.0691522

0.00335735 Yes

To Isom Composition.Benzene 0.0133051 0.0187839

0.00547876 Yes

To Isom Composition.Hydrogen 0.432842 0.429074

0.00376784 Yes

To Isom Composition.n-Hexane 0.0130054 0.0158849

0.00287947 Yes

To Isom Input Composition.110-120* 0.0960638 0.0926776

0.0033862 Yes

To Isom Input Composition.90-100* 0.0725096 0.0691528

0.00335681 Yes

To Isom Input Composition.Benzene 0.0133051 0.0187839

0.00547878 Yes



To Isom Input Composition.Hydrogen 0.432842 0.429077

0.00376519 Yes

To Isom Input Composition.n-Hexane 0.0130054 0.0158849

0.0028795 Yes

Total C3 Flow 804.157 801.361 kg/h 0.347704% Yes

Total C4 Flow 8046.71 8359.46 kg/h 3.886637% Yes

Total C4 Composition.110-120* 0.232798 0.22558

0.00721725 Yes


0.00104969 Yes


0.0020929 Yes


0.00862152 Yes

Total C4 Composition.Benzene 0.0456511 0.0642589

0.0186078 Yes

Total C4 Composition.i-Butane 0.0856589 0.0822307

0.00342813 Yes

Total C4 Composition.i-Pentane 0.0345026 0.0325087

0.00199399 Yes

Total C4 Composition.n-Butane 0.0531634 0.0512716

0.00189179 Yes

Total C4 Composition.n-Hexane 0.03806 0.0453341

0.00727407 Yes

Total Fuel Gas Flow 345.059 334.657 kg/h 3.014455% Yes

Total Fuel Gas Composition.Ethane 0.285184 0.292461

0.00727753 Yes

Total Fuel Gas Composition.Hydrogen 0.58722 0.576999

0.0102215 Yes

Total Fuel Gas Composition.Methane 0.127575 0.130518

0.00294288 Yes

Unstab Platformate Flow 47833.5 48182 kg/h 0.728593% Yes

Unstab Platformate Composition.110-120* 0.1723 0.16777

0.00453041 Yes


0.00367718 Yes


0.002677 Yes


0.00273119 Yes

Unstab Platformate Composition.Benzene 0.00945463 0.0134915

0.0040369 Yes

Unstab Platformate Composition.n-Hexane 0.0064345 0.00791774

0.00148324 Yes


Comment: The differences found are due to updated mapping in the feed stream going into the Isom Unit

subflowsheet in V8.0. The mapping was not monotonically increasing in V7.3, and this was corrected in V8.0 and

the change affects results.

aspen hysys v8 test case certification 21 jan 13-final

Documents

aspen hysys v8

certification test file

aspen hysys v7

test procedure

aspen plus

set of canned test files

certification testing

example files