Heat Exchangers, 2. Heat Transfer for Heat Exchanger Design

Abstract

The article contains sections titled: 1. Basic Heat‐Transfer and Pressure‐Drop Analysis 1.1. Basic Equations and Definitions of Heat‐Transfer Analysis 1.1.1. Fundamental Concepts 1.1.2. Temperature Distributions and Heat Exchanger Effectiveness 1.2. Dimensionless Methods for Exchanger Heat‐Transfer Analysis 1.3. Extensions of the Basic Heat‐Transfer Theory 1.3.1. Longitudinal Wall Heat Conduction 1.3.2. Variable Overall Heat‐Transfer Coefficients 1.4. Exchanger Pressure‐Drop Analysis 1.4.1. Plate – Fin Exchangers 1.4.2. Tube – Fin Exchangers 1.4.3. Regenerators 1.4.4. Plate Heat Exchangers 2. Single‐Phase Heat‐Transfer and Pressure‐Drop Correlations 2.1. Basic Concepts and Dimensionless Groups 2.2. Theoretical Solutions and Correlations for Simple Geometries 2.2.1. Fully Developed Flows 2.2.2. Hydrodynamically Developing Flows 2.2.3. Thermally Developing Flows 2.2.4. Simultaneously Developing Flows 2.3. Empirical Correlations for Complex Geometries 2.3.1. Tubular Exchangers 2.3.2. Plate Exchangers 2.3.3. Extended Surface Exchangers 3. Two‐Phase Heat‐Transfer and Pressure‐Drop Correlations 3.1. Flow Patterns 3.2. Two‐Phase Pressure‐Drop Correlations 3.2.1. Intube Pressure Drop 3.2.2. Shellside (Tube Bundle) Pressure Drop 3.2.3. Other Geometries 3.3. Heat‐Transfer Correlations for Condensation 3.3.1. Condensation Inside a Horizontal Tube 3.3.2. Condensation Inside a Vertical Tube 3.3.3. Condensation Outside Horizontal Tube Bundles 3.3.4. Condensation over Finned Tubes 3.3.5. Condensation Outside Vertical Tube Bundles 3.3.6. Condensation of Mixtures 3.4. Heat‐Transfer Correlations for Boiling and Evaporation 3.4.1. Intube Forced Convective Boiling 3.4.2. Intube Critical Heat Flux 3.4.3. Shellside Forced Convective Boiling 3.4.4. Shellside Critical Heat Flux 4. Thermal Design for Single‐Phase Heat Exchangers 4.1. Introduction 4.2. Shell‐and‐Tube Exchangers 4.2.1. Segmental Baffles 4.2.1.1. Shellside Heat Transfer 4.2.1.2. Shellside Pressure Drop 4.2.2. Disk‐and‐Doughnut Baffles 4.2.3. Rod Baffles 4.2.4. Design Procedure 4.3. Compact Heat Exchangers 4.3.1. The Rating Problem 4.3.2. The Sizing Problem 4.3.3. Micro‐Channel Heat Exchangers

Vinyl Chloride Recovery in a Multitubular Adsorber on Maxsorb Carbon

“…All feed reference values were supplied by Shin-Etsu CIRES, Estarreja, Portugal. Additionally, as described by Regufe et al, 2 mm pellet-shaped Maxsorb adsorbent will be used in the design of the unit. The proposed MT-TPSA cycle will operate in a temperature range of 303–393 K and a pressure range of 1–2.5 bar, limiting the use of vacuum pumps.…”

“…The MTA was designed by adapting the typical values found in the literature for shell and tube heat exchangers . The shell-side heat transfer coefficient and the heating fluid pressure drop were calculated following the Bell-Delaware method. , …”

Vinyl Chloride Recovery in a Multitubular Adsorber on Maxsorb Carbon

“…All feed reference values were supplied by Shin-Etsu CIRES, Estarreja, Portugal. Additionally, as described by Regufe et al, 2 mm pellet-shaped Maxsorb adsorbent will be used in the design of the unit. The proposed MT-TPSA cycle will operate in a temperature range of 303–393 K and a pressure range of 1–2.5 bar, limiting the use of vacuum pumps.…”

“…The MTA was designed by adapting the typical values found in the literature for shell and tube heat exchangers . The shell-side heat transfer coefficient and the heating fluid pressure drop were calculated following the Bell-Delaware method. , …”

A Hybrid Metaheuristic–Deterministic Optimization Strategy for Waste Heat Recovery in Industrial Plants

“…This is due to temperature differences and film heat transfer coefficients between process streams. Furthermore, in the industry, there is a large versatility of heat exchangers that range in size from small (0.1 m 2 ) to supergiant (over 10 5 m 2 ) …”

Optimal distribution of metal foam inserts in a double-pipe heat exchanger

“…This figure shows that at lower permeabilities, the effectiveness of the exchanger is higher. To perceive the impact of the porous inserts on the effectiveness of the heat exchanger, the effectiveness of a plain double-pipe, counter-flow heat exchanger at similar conditions is evaluated using equation (24) (Shah and Sekulic, 2003) and presented in Figure 12. From this figure, the superiority of the porous inserted heat exchanger is clear: …”

Vinyl Chloride Recovery in a Multitubular Adsorber on Maxsorb Carbon

“…All feed reference values were supplied by Shin-Etsu CIRES, Estarreja, Portugal. Additionally, as described by Regufe et al, 2 mm pellet-shaped Maxsorb adsorbent will be used in the design of the unit. The proposed MT-TPSA cycle will operate in a temperature range of 303–393 K and a pressure range of 1–2.5 bar, limiting the use of vacuum pumps.…”

“…The MTA was designed by adapting the typical values found in the literature for shell and tube heat exchangers . The shell-side heat transfer coefficient and the heating fluid pressure drop were calculated following the Bell-Delaware method. , …”

A Hybrid Metaheuristic–Deterministic Optimization Strategy for Waste Heat Recovery in Industrial Plants

“…This is due to temperature differences and film heat transfer coefficients between process streams. Furthermore, in the industry, there is a large versatility of heat exchangers that range in size from small (0.1 m 2 ) to supergiant (over 10 5 m 2 ) …”

Optimal distribution of metal foam inserts in a double-pipe heat exchanger

“…This figure shows that at lower permeabilities, the effectiveness of the exchanger is higher. To perceive the impact of the porous inserts on the effectiveness of the heat exchanger, the effectiveness of a plain double-pipe, counter-flow heat exchanger at similar conditions is evaluated using equation (24) (Shah and Sekulic, 2003) and presented in Figure 12. From this figure, the superiority of the porous inserted heat exchanger is clear: …”

Vinyl Chloride Recovery in a Multitubular Adsorber on Maxsorb Carbon

“…All feed reference values were supplied by Shin-Etsu CIRES, Estarreja, Portugal. Additionally, as described by Regufe et al, 2 mm pellet-shaped Maxsorb adsorbent will be used in the design of the unit. The proposed MT-TPSA cycle will operate in a temperature range of 303–393 K and a pressure range of 1–2.5 bar, limiting the use of vacuum pumps.…”

“…The MTA was designed by adapting the typical values found in the literature for shell and tube heat exchangers . The shell-side heat transfer coefficient and the heating fluid pressure drop were calculated following the Bell-Delaware method. , …”

A Hybrid Metaheuristic–Deterministic Optimization Strategy for Waste Heat Recovery in Industrial Plants

“…This is due to temperature differences and film heat transfer coefficients between process streams. Furthermore, in the industry, there is a large versatility of heat exchangers that range in size from small (0.1 m 2 ) to supergiant (over 10 5 m 2 ) …”

Optimal distribution of metal foam inserts in a double-pipe heat exchanger

“…This figure shows that at lower permeabilities, the effectiveness of the exchanger is higher. To perceive the impact of the porous inserts on the effectiveness of the heat exchanger, the effectiveness of a plain double-pipe, counter-flow heat exchanger at similar conditions is evaluated using equation (24) (Shah and Sekulic, 2003) and presented in Figure 12. From this figure, the superiority of the porous inserted heat exchanger is clear: …”