- #Aspen hysys how to#
- #Aspen hysys pdf#
- #Aspen hysys full#
- #Aspen hysys simulator#
- #Aspen hysys windows#
With this you can access the specific options of each unit if you know the path. Hysys.UO is a dictionary with the connection to the unit operations.
#Aspen hysys full#
Hysys.EnergyStreams is the connection to energy streams in case you want to use (and know) the full path to the variable of interest here.Ħ. Hysys.MaterialStreams is the connection to material streams in case you want to use (and know) the full path to the variable of interest here.ĥ. This is specially useful to turn it ON/OFF when changing input values to the simulation.Ĥ. Hysys.Solver is the solver in Aspen HYSYS. Hysys.SS is a dictionary with the connections to the spreadsheets.ģ.
So you can work directly on spreadsheets.Ģ. As I said, this is sometimes problematic.
#Aspen hysys pdf#
To find this paths you can use the "Object browser" from Excel VBA or Matlab and the "HYSYS Customization Guide" pdf file. From here you can access all the variables usign the specific variable paths. Hysys.H圜ase is the complete Aspen HYSYS case. This is helpful for students, teachers, engineers and researchers in the area of R&D, specially those.
#Aspen hysys how to#
The output is a class Hysys with the following methods:ġ. Aspen HYSYS - Petroleum Assays and Oil Characterization (Slideshare) This is course on Plant Simulation will show you how to setup hypothetical compounds, oil assays, blends, and petroleum characterization using the Oil Manager of Aspen HYSYS.
active whether the Aspen HYSYS file is currently active or not.
#Aspen hysys simulator#
hy_visible whether to make Aspen HYSYS visible or not. Aspen HYSYS (or simply HYSYS) is a chemical process simulator used to mathematically model chemical processes, from unit operations to full chemical plants and refineries. ('Cooler', 'Flash Drum', 'Heater', 'Valve', 'Reactor', 'Distillation Column', 'Turbine', 'Pump')Ĥ. This is useful for example when dealing with distillation columns and their specific flowsheet window.Į.g. Unit_operation_name is a list of the names of the unit operations present within the Aspen HYSYS file. ('SS_Flash', 'SS_turbine', 'SS_Distillation')ģ.
#Aspen hysys windows#
Spreadsheet_name is a list of names for the specific spreadsheets within the Aspen HYSYS file that we are connecting with Python.Į.g. Under the Windows icon, go to the Aspen HYSYS folder, and click on the Aspen HYSYS program icon, as indicated below. File_name of the Aspen HYSYS file you are working with.Ģ. There are still challenges in improvement of the simulation robustness and the cost estimation accuracy.Aspen_connection(File_name, Spreadsheet_name, Unit_operation_name, hy_visible=1, active=0)ġ. The combination of Aspen HYSYS and Aspen ICARUS is a good tool for evaluating different process configurations. The split-stream alternative also becomes more attractive when the energy cost increases. With a period above 20 years the split- flow becomes most economical. The split-stream alternative becomes more attractive when the calculation period increases. It means that the split-flow configuration is not economically attractive for 10 years period. The investment cost was increased with 212 MNOK due to added complexity of the process with split- stream and the operation cost for a period of 10 years was reduced with 139 MNOK. With a steam cost of 0.1 NOK/(kWh) the energy net present value for this process for a period of 10 years was 975 MNOK. The total installed equipment cost of the selected standard CO2 removal process without split-stream was 760 MNOK. Equipment cost estimations were calculated in Aspen ICARUS. In this case a heat exchanger minimum temperature difference was 5K. It was possible to further reduce reboiler energy consumption for the case with split- stream down to 3.0 MJ/kg with 26 stages in the absorber. 3.4 MJ/kg was achieved for the process with split-stream and 24 absorber stages. The reboiler duty of 3.8 MJ/kg CO2 removed for the standard process without split-stream was achieved with 18 absorber stages. For the selected base cases the heat exchanger minimum temperature difference was specified to 10K and the removal efficiency was 85%. The model has been calculated with variation of parameters to optimize the process and find an optimum solution.
An Aspen HYSYS model of CO2 removal was developed and modified with a split-stream configuration in order to reduce energy consumption in the reboiler.