M.Sc Student | Ben-Zvi Itai |
---|---|

Subject | Study of Sub Critical Pure Coolant Joule-Thomson Cryocooler Including Condensation inside the Recuperator |

Department | Department of Mechanical Engineering |

Supervisors | Assistant Professor Michael Shusser |

Professor Emeritus Gershon Grossman | |

Dr. Benzion Meital | |

Full Thesis text - in Hebrew |

Most cryocoolers based on the Joule - Thomson principle use pure gases and operate at high pressures. Using gas mixtures enables working at sub- critical, low pressures and gains some workability advantage. Operating cryocoolers at sub- critical pressure causes condensation and liquid phase is formed along the heat exchanger. Better understanding and improvement of cryocoolers operated at sub- critical pressures could be achieved by solving the flow and temperature fields at the heat exchanger including the evolution of the liquid layer.

In this work a numerical solution is developed to predict heat and mass transfer at JT cryocoolers that use pure gases at sub- critical pressures. The work is a preliminary step for solving gas mixture problems.

A counter-flow laminar heat exchanger consisting of two concentric pipes is considered. Mass, momentum and energy equations were solved numerically by using the integral method.

A computer program was written that allows to solve the concentric pipe counter flow heat exchanger for any pure substance.

The model ability to analyze performance of JT cryocoolers is demonstrated. Main conclusions obtained by applying the model are as follows:

· There is a minimum of the radial heat flux at gas-liquid boundary in the part of the heat exchanger where the condensation occurs.

· Predictions of the NTU method and the current model for a two phase heat exchanger are compared. The NTU model predicts no condensation at all, even where the current model shows significant liquid layer evolution.

·
There
is an optimal value of the parameter *ξ*=*Δh/ Δh _{T}
≤*1 (ratio of the enthalpy difference in the heat exchanger to the
maximum possible enthalpy difference) for which the length of the heat
exchanger is minimal. This value of

·
The
length of the heat exchanger depends also on pipes geometry. The length is
influenced only by the ratio of the pipe radii,* η _{m}=R_{o}/
R_{i}* ≥1. Varying the pipe radii while keeping the ratio
constant does not change the heat exchanger length. For smaller