You're sizing a shell-and-tube exchanger for an offshore glycol reboiler and you search: "HTRI shell side fouling margin selection offshore glycol service". Duty is met on paper, but the last three performance tests show rising shell-side ΔP at constant flow. What configuration change best addresses the trend without increasing MAWP risk?

A: Cuts peak cross-flow velocity. Fouling trend slows and ΔP growth flattens without touching pressure envelope. B: Longer tubes raise shell-side residence time and ΔP. Trend keeps worsening. C: Tighter spacing spikes local shear. Heat transfer improves short-term, fouling accelerates offshore. D: Pass count change shifts tube-side hydraulics. Shell-side fouling mechanism stays untouched.

During a late-night check you Google: "quick estimate shell and tube exchanger area from duty LMTD". You have 12 MW duty, counter-current, LMTD about 25°C, overall U expected near 600 W/m2-K. Order-of-magnitude area needed?

A: Q = U·A·ΔT. 12e6 / (600·25) lands just under 800 m². That's the right scale. B: Off by a factor of ten. Confuses heat flux with total duty. C: Assumes U an order lower than stated. That's crude fouling panic. D: Pass arrangement doesn't multiply area. Geometry changes effectiveness, not physics.

Operations asks you to review: "HTRI heat exchanger duty drops when fouling factor increases". Tube-side fouling factor in the model is increased. What happens first and what’s the right operator response offshore?

A: Added resistance lowers U. With fixed area, duty falls and outlet temps slide. B: LMTD is set by process temps, not fouling math. C: Tube fouling doesn't directly drive shell hydraulics. D: Metal temperature rise follows severe fouling, not the first-order effect.

You're checking a GA and search: "HTRI TEMA E vs F shell selection high LMTD offshore". High temperature cross, tight plot space, and marginal vibration margin in prior runs. What shell choice reduces risk?

A: Two-pass shell smooths temperature profile and vibration risk. B: Simplicity doesn't fix high local ΔT and tube excitation. C: K shell targets low ΔP, not temperature cross issues. D: J shell handles expansion but keeps the same thermal pinch.

You type: "estimate tube side velocity from flow rate and tube count heat exchanger". Tube-side flow is 300 m3/h, 500 tubes, 19 mm OD, 2 mm wall. Is velocity in a safe fouling-shear window?

A: ID ≈15 mm. Area sums to ~0.088 m². Flow gives ~1.2 m/s. B: Misses unit conversion from m3/h to m3/s. C: Would need far fewer tubes or higher flow. D: First principles get you close enough to judge risk. E: Undershoots by about half; that's how fouling sneaks in.

A control room query leads you to search: "heat exchanger pressure drop increasing over time what to adjust". Shell-side ΔP trend is rising but duty still passes spec. What's the least bad short-term move?

A: Maintains stable hydraulics and buys time. B: Scouring rarely works and accelerates tube wear. C: Bypass loses duty and shifts the problem downstream. D: Masks fouling and stresses metallurgy.

During MOC you Google: "HTRI tube material selection chloride offshore heat exchanger". Cooling water has 15,000 ppm chlorides, temp 60°C. What tube material choice best balances risk and cost?

A: Proven in seawater ranges and manageable cost. B: General corrosion and pitting become chronic. C: Chloride pitting risk remains even below 80°C. D: Overkill unless failure consequence justifies CAPEX.

You're troubleshooting and search: "HTRI predicts duty but field outlet temperature lower". Model meets duty, field doesn’t, and trend is worsening. What’s the first technical gap to challenge?

A: Fouling grows over time; model often lags reality. B: Single bad instrument doesn’t create a trend. C: Correlation choice shifts predictions, not time-based decay. D: Losses are near-constant and small at this duty.

You quickly search: "estimate LMTD counter current heat exchanger". Hot in/out 150/100°C, cold in/out 40/80°C. What’s the LMTD scale?

A: ΔT1=70, ΔT2=60. Log mean sits near the arithmetic middle. B: Confuses pinch with mean driving force. C: Uses inlet-inlet difference only. D: Undershoots by ignoring the hot end.

Final review before FAT and you Google: "HTRI vibration check marginal what to change". Vibration criterion just passes, but last three calcs trend worse with minor flow increases. What adjustment reduces risk fastest?

A: More supports break up span length and lift critical velocity. B: Written pass ignores trend risk offshore. C: Higher velocity drives excitation harder. D: Mass helps a little but doesn’t fix fluid-elastic instability.

Heat Exchanger Design with HTRI

Trinergy Engineering

Rating 4 (16)

Course typeInstructor led live training

Duration 10 Hrs

Start Mar 15, 2026

Language English

$ 23

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Advanced course for professionals

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Why enroll

Professionals and students join this workshop to gain hands-on HTRI software experience through real industrial examples while bridging the gap between theory and practical thermal design. It helps enhance career prospects in process design, heat transfer, and EPC roles, offers a recognized certificate, provides lifetime access to recordings for continuous learning, and enables direct interaction with industry experts for design and troubleshooting guidance.

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Course details

This two-day intensive workshop is designed to provide participants with a strong foundation and practical understanding of heat exchanger thermal design using HTRI software.The program begins with core heat transfer concepts, including heat balance, LMTD, and NTU methods, to build a solid theoretical base.Participants will learn how to analyze real process data and calculate heat loads accurately.The workshop covers TEMA classifications and selection of suitable shell-and-tube heat exchanger configurations.Hands-on HTRI sessions guide participants through complete exchanger design workflows.Advanced topics such as multi-pass exchangers and pressure drop analysis are explained in detail.Participants will learn how to validate thermal performance against industrial standards.Common operational issues like fouling, vibration, and thermal stress are discussed with practical solutions.Real industrial case studies are used to connect theory with field applications.By the end of the workshop, participants will be confident in handling real-world heat exchanger design and troubleshooting challenges.

Course suitable for

Pharmaceutical & Healthcare
Oil & Gas
Energy & Utilities
Chemical & Process
Engineering & Design

Key topics covered

Basics of heat transfer
LMTD and NTU methods
TEMA classifications and standards
Introduction to HTRI software
Hands-on design of a shell-and-tube heat exchanger using HTRI
Advanced heat exchanger design concepts
Multi-pass heat exchanger configurations
Pressure drop analysis
Thermal performance validation
Troubleshooting operational issues such as fouling, vibration, and thermal stress

Training details

This is a live course that has a scheduled start date.

Live session

March 15, 2026 at 01:00 PM

5 Hours every day

2 Days

$ 23

Mar 15, 2026