Evaluation Blocks

Navigation: Models ➔ Sub-Models ➔ Evaluation Blocks

Project, Model and Solver Settings				Simulation Modes and Solver Setup			Solver Methodology, Convergence and Tolerance				Solving Models
Project Settings	Solver Settings	Plant Model	Constants	Simulation Modes	ProBal Setup	Dynamic Setup	Solver Status	Solver Methodology	Convergence Methods	Tolerance Testing	Evaluating Sub-Models	Flash Train	Mass & Energy Balance	Referenced Variables	Demand

General Description

An Evaluation Block (EB) gives the user a quick and convenient way to introduce commonly used functionality for things like chemical reactions, phase change and environmental heat loss into unit operations in a generic manner. There are some limitations on what can be done with the EB, but overall it is a powerful tool.

An EB is a set of sub-models with a controller for managing them. The EB control allows sub-models to be turned on or off by the user and allows the user to choose the evaluation order of the sub-models. Evaluation blocks are available in pipes, ties, tanks and some unit operations. They are available in both ProBal and Dynamic modes and work exactly the same way in both.

The sub-models act on the flow in a pipe, a tie, a tank or the feed stream to a unit operation model. For ties, tanks and most units, the EB acts on the combined feed flow. Typically, the sub-models available in an evaluation block include Makeup Block (MU), Reaction Block (RB), Environmental Heat Exchange EHX, Evaporation Block (Evap) and Vapour Liquid Equilibrium VLE. However, not all sub-models are available in all units and in some units some of the sub-models are available separately from the EB. There is also a Phase Change sub-model that may be available in the EB, if it has NOT already been enabled globally in Plant Model.

The sub-models are evaluated sequentially. This means that to some extent the answer may depend on the order in which the sub-models are evaluated (as explained below).

The general calculation procedure is that all of the feed streams and all of the makeup streams are mixed together and the pressure of the mixed stream is adjusted to the product pressure.
The product pressure is determined by the pressure sub-model associated with the particular unit operation (the pressure models sit outside of the EB and there are different options depending on the unit).
Enthalpy is conserved during the mixing and pressure adjustment process and the temperature is adjusted so that the enthalpy flux of the EBFeed matches the sum of the feed and makeup enthalpy fluxes into the unit.
This mixed, pressure adjusted stream is the EBFeed stream.

The various sub-models then act on the EBFeed stream in series. In effect the EBFeed stream is passed to the first sub-model which acts upon it, then the product stream from this sub-model (the modified EBFeed stream) is passed to the next sub-model and so on. In the example below, a feed stream with makeups is mixed and the pressure is adjusted. It then has the chemical reaction, environmental heat transfer and VLE sub-models acting on it.

All feed streams are mixed and the pressure is adjusted based on the required pressure method. This sets the EBFeed Temperature.
The temperature to the Rxn sub-model is the EBFeed temperature.
The temperature and composition out of the reaction sub-model are determined by the reaction extents and the heat of reaction.
The feed stream to the EHX sub-model has this composition and temperature.
The heat loss from the EHX sub-model is determined using the feed temperature to the sub-model and the ambient temperature. The enthalpy of the outlet stream is adjusted for the heat loss to determine the exit temperature. #This stream then feeds the VLE sub-model where flashing or condensation occur to match the given product pressure and stream enthalpy.

The sequence in which these models act can affect the calculated result. For example if a particularly energetic reaction occurs then the temperature out of the reaction sub-model to the EHX sub-model may be significantly different than the feed temperature to the unit and the EHX calculated result will be different than if the EHX sub-model had been called first. In general, this is not usually a problem and often for scenarios where sub-model sequence would be an issue there is an existing dedicated unit operation that solves all of the relevant equations simultaneously. NB as a general rule, VLE should be called last.

Sequencing

Sub-models may be switched on by selecting one of the On options from the drop down menu. They are off by default.

If the user chooses On-AutoSequence then SysCAD will determine the sequence of the sub-models. The auto sequence followed will be Makeups, RB, EHX, Evap, VLE, Discards.

If the user wishes to override this sequence, they can choose the order, On-Sequence1 for the first sub-model, On-Sequence2 for the second sub-model, etc. Note that if any sub-models are left as On-AutoSequence these are always first in the order. If two or more sub-models have the same Sequence number then the auto sequence will be followed within this group of equal sequence.

The evaluation sequencing for the Phase Change sub-model works somewhat differently than the other sub-models. The phase change sub-model is evaluated after the initial mixing of all the feed and makeup streams and then again after each of the other active sub-models acts on the stream. It may act on the stream multiple times when multiple other sub-models are used and it is always the last sub-model to act on the stream.

When the reaction sub-model is enabled along with other sub-models and reaction extent is controlled based on some final value (for example final concentration), then the user may need to use a PID controller to adjust the extent of reaction. For example, if we have the reaction A -> B and the reaction extent is controlled to give a final concentration of B and we also have the VLE sub-model acting afterwards. Then if a significant amount of solvent is flashed off, the final concentration may not be correct since the concentration of B will increase as solvent is flashed to vapour. This can be overcome by using a PID with the target concentration as the set point, the actual concentration of B in the product stream as the measured value and allowing the PID to adjust the reaction extent in the sub-model to give the desired value. A separate PID can be used for each reaction.