Fauske

The minimum capacity of quench liquid can be estimated by a heat balance, knowing the final quench pool temperature. The following equation given by Fauske Intemational Symposium on Multi-Phase Transpoii and Paiiiculate Phenomena, December 15-17, I9S6) can be used to calculate the minimum amount of quench hquid ... 

The vent sizing package (VSP) was developed by Fauskes Associates, Inc. The VSP and its latest version VSP2 employ the low thermal mass test cell stainless steel 304 and Hastelloy test cell with a volume of 120 ml contained in a 4-1, high-pressure vessel as shown in Figure 12-13. The typical ([t-factor is 1.05-1.08 for a test cell wall thickness of 0.127-0.178 mm. Measurements consist of sample temperature Tj and pressure Pj, and external guard temperature Tj and... 

Figure 12-13. Vent sizing package (VSP) apparatus. (Source Fauskes Associates Inc.)...

Fauskes Assoeiates Ine. developed the RSST as an inexpensive sereening tool [15,16]. The RSST (Figures 12-14 and 12-15) eonsists of a spherieal glass reaetion vessel and immersion heater (optional). 

Fauske [29] developed a simplified ehart for the two-phase caleula-tion. The relief area was expressed as ... 

Fauske [32] represented a nomograph for tempered reaetions as shown in Figure 12-35. This aeeounts for turbulent flashing flow and requires information about the rate of temperature rise at the relief set pressure. This approaeh also aeeounts for vapor disengagement and frietional effeets ineluding laminar and turbulent flow eonditions. For turbulent flow, the vent area is... 

It is reeommended that a safety faetor of at least 2.0 be used [34]. In eertain eases, lower safety faetors may be employed. The designer should eonsult the appropriate proeess safety seetion in the engineering department for adviee. Table 12-4 lists the applieability of both Leung and Fauske s methods. 

If Fauske s method yields a signifieantly different vent size, then the ealeulation should be reviewed. 

The answer obtained from the Leung s method should not be signifieantly smaller than that of Fauske s method. 

Fauske, El. K., Clare, G. El., and Creed, M. J., Lahoratory Tool for Charaeterizing Chemieal Systems, Proeeeding of tlie Int. Symp. on Runaway Reaetions, AIChE/CCPS, Boston, MA, Mareh 7-9, 1989. 

Fauske, H. K., Generalized Vent Sizing Monogram for Runaway Chemieal Reaetions, Plant/Operation, Prog., Vol. 3, No. 3, Oetober 1984. 

Fauske, H. K., Emergeney Relief System Design for Runaway Chemieal Reaetion Extension of the DIERs Methodology, Chem. Eng. Res. Des., Vol. 67, pp. 199-202, 1989. 

Fauske, H. K. and M. Epstein, 1988, Source Term Considerations in Connection with Chemical Accidents and Vapor Cloud Modeling, Proceedings of the International Conference on Vapor Cloud Modeling, CCSP, 251-273. 

Heni, R. E. and H. K. Fauske, 1971, The Two-Phase Critical Flow of One-Component Mistuies in Nozzles, Orifices, and Short Tubes, J. Heat Transfer, pp 179-187, May. 

Regarding two pliase flow, pressurized liquid above its noniial boiling point will start to flash when released to aUiiospheric pressure, and two pliase flow will result. Two-pliase flow is also likely to occur from depressurization of tlie vapor space above a volatile liquid, especially if the liquid is viscous (e.g., greater tlian 500 cP) or has a tendency to foam. Fauske and Epstein liave provided tlie following practical calculation guidelines for two-phase flashing flows. The discharge of subcooled or saturated liquids is described by... 

Figure 7-61. Reactive system screening tool (RSST) for evaluating runaway reaction potential. By permission, Fauske and Associates, Inc.

The Fauske and Associates Reactive System. Screening Tool (RSST) w as developed as a result of the DIERS studies and allow s rapid evaluadon of the potential for runaway reactions. It measures the rate of energy and gas release during the runaway and is valuable for screening various process s)stems before commercial designs are completed (see Figure 7-61). 

There is no standardized method for predicting or controlling runaw ay reaction that may lead to explosions (deflagrations or detonations), except possibly the Fauske approach (Figure 7-61). 

Fauske, H. K., M. A. Grolmes, and G. LI. Glare, Process Safety Evaluation Appl) ing DIERS Mediodolog) to Existing Plant Operations, Plant Operations Progress, Vol. 8, No. 1, 1989, p. 40. 

Leung, J. C. and Fauske, H. K, Runaway System Characterization and Vent Sizing Based on DIERS Methodology, Plant Operations Progress, V. 6, No. 2, 1987, p. 77. 

Fauske, H. K., Emergency- Relief System Design for Reactive and Non-Reactive Systems Extension of the DIERS Methodology, Plant/Operations Prog., V. 7, No. 3, 1988, p. 153. 

Grolmes, M. A. and Fauske, H. K., An Evaluation of Incomplete Vapor-Phase Separation in Freon-12 Top Vented Depre-ssurization Experiments, Multi-Phase Flow and Heat Transfer III. Part A Fundamentals. Proceedings of the Third Multi-Phase Flotv and Heat Transfer Symposium-Workshop, Miami Beach, FL, April 18-20, 1983. 

Fauske, H. K, et al, Emergency Relief Vent Sizing for Fire Emergencies Invoking Liquid-Filled Atmospheric Storage Vessels, Plant/Operations Progress, 5 (4), 205-208, October 1986. 

Epstein, M., Fauske, H. K. and Hauser, G. M., The Onset of Two-Phase Venting Via Entr ainment in Liquid-Filled Storage Vessels Exposed to Fire, Journal Loss Prevention Process Industries, 2 (1), 45-49, January 1989. 

Fauske and Associates, Inc., Flashing Viscous Flow of Polystyrene Mixtures Test Data and Scale-Up Methods, FAI/ 89-26, April 1989. 

Fauske, H. K., Scale-up for Safety Relief of Runaway Reactions, Plant/Operalions Progress, 3 (1), 7-11, January 1984. 

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