### Part 2: Hydrogen Turbomachinery Design

Hydrogen is attracting a lot of interest in different circles these days from: propulsion, to energy storage, to personal transportation. The most obvious benefit of hydrogen fuel is a total lack of...

A blog on what's new, notable, and next in turbomachinery

**The Refprop program**

The calculations in the National Institute of Standards and Technology (NIST) *Refprop* program are generally considered the most accurate thermo-fluid models available. The routines are widely used in many applications.

**The models**

Several different models are embedded in the *Refprop* formulation. The most important are the Benedict-Webb-Rubin equations of state for the pressure-temperature-density relationship.

The equation takes this form:

This is clearly way more complicated than the corresponding cubic implementation (Going Through a Phase – Modeling Phase Change with Cubics). Other equations get even more complex since many of these require various integrations and derivatives of this already complex equation.

**Application**

The *Refprop* calculations are considered to be the only formulation accurate enough to predict fluid properties near the difficult critical point. The plot, taken from Refprop itself (below), shows the critical point on a temperature vs. entropy plot (left) and z (compressibility) vs. pressure curve (right). The properties near the critical point are particularly nonlinear and change very rapidly, hence the challenge in calculating them.

Encountering flow conditions near the critical point is actually quite rare. The high temperatures and pressures of most fluids at the critical point tend to be quite difficult to handle. New cycles which take advantage of fluid behavior near the critical point are actively being investigated though. Carbon dioxide, in particular, has attracted a lot of interest since its critical point is found at a reasonably low temperature.

**The issues**

As good as the *Refprop* calculations are, there are two important issues the user needs to consider when using it. The most important issue is the very slow run time. A CFD solver might make millions or possibly even billions of calls to the thermodynamic routines to the so-called equation of state (EOS) in the course of a solution. The computationally intensive *Refprop* calculation can eat up huge amounts of computational time in this situation. Several publications have documented CFD runtime increases more than 50 times when run with direct calls to *Refprop*. To get past this, most applications use a computational efficient interpolation scheme populated with NIST-derived data.

The second issue is that *Refprop* is quite unyielding outside its designated range. If a solver asks for something outside the tightly designed range limits, *Refprop* will refuse to answer. In programming terms, that means the dreaded NaN (not-a-number). While this could be considered an advantage, not to answer when outside the proper definition, it can be quite limiting. Many solvers iterate over a wide range of states before settling down to a more narrowly defined range. If any calls fail during any of these iterations, then the solution is done. This is true even if the solver might ultimately settle in a valid region after it stabilizes. Trapping these errors is necessary for all but the most stable and predictable iteration schemes.

Blogs in this series:

Fluid Phenomena Primer: Energy Versus Temperature, Specific Heat

__Phase Change - Make Mine a Double!__

When Perfect is Good Enough - Perfect Gas Models

__What's Better than Perfect? Semi-Perfect Gas Models__

__Going Through a Phase – Modeling Phase Change with Cubics__

**Tags:**
Engineering

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