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Abstract. This paper presents experimental results for pressure drop during air-water upward two-phase flow across horizontal triangular tube bundle. It is estimated that more than half of shell-and-tube heat exchangers in industry operate under two-phase flow conditions in the shell side. However the number of research and publications focused on external flow is considerably reduced when compared to intube flow. This study addresses experimental results for pressure drop during external flow of air and water mixtures across a triangular tube bundle counting with 19 mm OD tubes and 24 mm transverse pitch, for superficial velocities up to 0.553 and 10 m/s for water and air, respectively. For reduced mass velocities, the gravitational pressure drop parcel is dominant, consequently the adoption of an appropriate methodology for void fraction estimative is essential for accurate estimative of the gravitational pressure drop parcel. The experimental results are compared with predictive methods available in the open literature, and an analysis of this comparison is presented.
Abstract. This paper presents experimental results for pressure drop during air-water upward two-phase flow across horizontal triangular tube bundle. It is estimated that more than half of shell-and-tube heat exchangers in industry operate under two-phase flow conditions in the shell side. However the number of research and publications focused on external flow is considerably reduced when compared to intube flow. This study addresses experimental results for pressure drop during external flow of air and water mixtures across a triangular tube bundle counting with 19 mm OD tubes and 24 mm transverse pitch, for superficial velocities up to 0.553 and 10 m/s for water and air, respectively. For reduced mass velocities, the gravitational pressure drop parcel is dominant, consequently the adoption of an appropriate methodology for void fraction estimative is essential for accurate estimative of the gravitational pressure drop parcel. The experimental results are compared with predictive methods available in the open literature, and an analysis of this comparison is presented.
The article contains sections titled: 1. Introduction 2. Classification of Heat Exchangers 2.1. Classification According to Construction 2.1.1. Tubular Heat Exchangers 2.1.1.1. Shell‐and‐Tube Exchangers 2.1.1.2. Double‐Pipe Heat Exchangers 2.1.1.3. Drip‐Type Heat Exchangers 2.1.2. Plate‐Type Heat Exchangers 2.1.2.1. Plate Heat Exchangers 2.1.2.2. Spiral‐Plate Heat Exchangers 2.1.3. Extended‐Surface Heat Exchangers 2.1.3.1. Plate ‐ Fin Heat Exchangers 2.1.3.2. Tube ‐ Fin Heat Exchangers 2.1.4. Regenerators 2.2. Classification According to Process Function 2.2.1. Condensers 2.2.2. Liquid‐to‐Vapor Phase‐ChangeExchangers 2.2.2.1. Chemical Evaporators 2.2.2.2. Reboilers 2.2.2.3. Waste Heat Boilers 3. Heat Exchanger Design Methodology 4. Criteria for Heat Exchanger Selection 4.1. General Selection Criteria 4.1.1. Design Variables 4.1.2. General Selection Guidelines 4.2. Shell‐and‐Tube Exchangers 4.2.1. Tubes 4.2.2. Tube Pitch and Layout 4.2.3. Baffles 4.2.4. Shells 4.2.5. Front‐End Heads 4.2.6. Rear‐End Heads 4.2.7. Nozzles 5. Basic Heat‐Transfer and Pressure‐Drop Analysis 5.1. Basic Equations and Definitions of Heat‐Transfer Analysis 5.2. Dimensionless Methods for Exchanger Heat‐Transfer Analysis 5.3. Extensions of the Basic Heat‐Transfer Theory 5.3.1. Longitudinal Wall Heat Conduction 5.3.2. Variable Overall Heat‐Transfer Coefficients 5.4. Exchanger Pressure‐Drop Analysis 5.4.1. Plate ‐ Fin Exchangers 5.4.2. Tube ‐ Fin Exchangers 5.4.3. Regenerators 5.4.4. Plate Heat Exchangers 6. Single‐Phase Heat‐Transfer and Pressure‐Drop Correlations 6.1. Basic Concepts and Dimensionless Groups 6.2. Theoretical Solutions and Correlations for Simple Geometries 6.2.1. Fully Developed Flows 6.2.2. Hydrodynamically Developing Flows 6.2.3. Thermally Developing Flows 6.2.4. Simultaneously Developing Flows 6.3. Empirical Correlations for Complex Geometries 6.3.1. Tubular Exchangers 6.3.2. Plate Exchangers 6.3.3. Extended Surface Exchangers 7. Two‐Phase Heat‐Transfer and Pressure‐Drop Correlations 7.1. Flow Patterns 7.2. Two‐Phase Pressure‐Drop Correlations 7.2.1. Intube Pressure Drop 7.2.2. Shellside (Tube Bundle) Pressure Drop 7.2.3. Other Geometries 7.3. Heat‐Transfer Correlations for Condensation 7.3.1. Condensation Inside a Horizontal Tube 7.3.2. Condensation Inside a Vertical Tube 7.3.3. Condensation Outside Horizontal Tube Bundles 7.3.4. Condensation over Finned Tubes 7.3.5. Condensation Outside Vertical Tube Bundles 7.3.6. Condensation of Mixtures 7.4. Heat‐Transfer Correlations for Boiling and Evaporation 7.4.1. Intube Forced Convective Boiling 7.4.2. Intube Critical Heat Flux 7.4.3. Shellside Forced Convective Boiling 7.4.4. Shellside Critical Heat Flux 8. Thermal Design for Single‐Phase Heat Exchangers 8.1. Introduction 8.2. Shell‐and‐Tube Exchangers 8.2.1. Segmental Baffles 8.2.1.1. Shellside Heat Transfer 8.2.1.2. Shellside Pressure Drop 8.2.2. Disk‐and‐Doughnut Baffles 8.2.3. Rod Baffles 8.2.4. Design Procedure 9. Thermal Design for Multiphase Heat Exchangers 9.1. Condensers 9.1.1. Considerations in Condenser Design 9.1.2. Condenser Types and Their Characteristics 9.1.2.1. Shellside Condensers 9.1.2.2. Tubeside Condensers 9.1.2.3. Air‐Cooled Condensers 9.1.3. Condensation of Mixtures 9.1.4. Mean Temperature Difference 9.1.5. Desuperheating 9.1.6. Subcooling 9.2. Vaporizers 9.2.1.
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