Process Equipment Design: Fundamentals and Applications

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Self-paced Advanced

Process Equipment Design: Fundamentals and Applications

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Trainers Rating: 3(118)
Course type: Watch to learn anytime
Duration: 1939 min
Start: Anytime
Language: English
Views: 1355

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Pharmaceutical & Healthcare

Chemical & Process

Why enroll

Upon completion, students will be able to design and analyze process equipment, considering safety, regulatory, and practical requirements.

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Engineering Academy

Project Engineer

Learn Without Limits: Free Engineering Courses

Total experience: 5+ years
Location: India

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Course details

Course suitable for

Is this course for you?

Perfect for

You work in Pharmaceutical & Healthcare
You're a Chemical & Process / Mechanical Engineering professional
You have 3+ years of hands-on experience in this field
You prefer self-paced learning you can revisit

Before you enrol

Advanced level — assumes working knowledge of Chemical & Process
Self-paced video, 1939 min — watch anytime

New to Chemical & Process? Browse beginner courses →

Ready for the next step?

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Course curriculum

The course is readily available, allowing learners to start and complete it at their own pace.

61 lectures32 hr 19 min

Introduction
5 min
Introduction of Process Equipment Design
43 min
Classification of exchangers-1
34 min
Classification of exchangers-2
42 min
Basic design parameters-1
37 min
Basic design parameters-2
40 min
Double pipe exchanger-1
34 min
Double pipe exchanger-2
41 min
Double pipe exchanger-3
25 min
Types of Shell and Tube exchangers
37 min
Exchanger Tubes
38 min
Exchanger Shell
33 min
STE design- Kern’s method-1
30 min
STE design- Kern’s method-2
31 min
STE design- Kern’s method-3
25 min
STE design- Kern’s method-Example-4
40 min
STE design- Kern’s method-Example-5
25 min
STE design- Bell’s method-1
36 min
STE design- Bell’s method-2
31 min
STE design- Bell’s method-3
33 min
STE design – Bell’s method: Example-4
32 min
STE design – Bell’s method: Example-5
29 min
Design of Condenser-1
33 min
Design of Condenser-2
38 min
Design of Condenser-3
31 min
Design of Condenser-4
31 min
Design of Condenser-5
22 min
Design of Reboiler-1
38 min
Design of Reboiler-2
36 min
Design of Reboiler-3
25 min
Design of Reboiler-4
29 min
Design of Reboiler-5
36 min
Design of Reboiler-6
34 min
Design of Reboiler-7
26 min
Design of Evaporator-1
35 min
Design of Evaporator-2
29 min
Design of Evaporator-3
28 min
Design of Evaporator-4
29 min
Design of Evaporator-5
33 min
Design of Crystallizer-1
31 min
Design of Crystallizer-2
29 min
Design of Crystallizer – Examples
32 min
Design of Crystallizer – Types
26 min
Design of Packed Column-1
29 min
Design of Packed Column-2
29 min
Design of Packed Column-3
36 min
Design of Packed Column-4
26 min
Design of Packed Column-5
31 min
Distillation Column – 1
34 min
Distillation Column – 2
30 min
Distillation Column – 3
35 min
Distillation Column – 4
30 min
Distillation Column – 5
34 min
Distillation Column – 6
24 min
Distillation Column – 7
35 min
Distillation Column – 8
34 min
Distillation Column – Mechanical Design-1
34 min
Distillation Column – Mechanical Design-2
28 min
Distillation Column – Mechanical Design-3
31 min
Distillation Column – Mechanical Design-4
32 min
Distillation Column – Mechanical Design-5
35 min

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✎ Where this fits — what comes before, what comes next

Frequently asked questions

Q: You're sizing a shell-and-tube exchanger and searching "shell and tube heat exchanger fouling factor for cooling tower water". Duty is 3.5 MW, cooling tower water on tube side, ΔP limit 70 kPa. Which fouling factor assumption is defensible at design?

A: 0.000035 m²·K/W is the boundary most vendors default to for treated tower water when velocities stay above about 1 m/s. Below that, fouling accelerates; above it, erosion becomes the limit. The other values either drop fouling without evidence, double-count conservatism, or misapply it by side.

Q: During SAT you're googling "API 610 pump field verification sequence before first start". OH2 pump, new piping, cold alignment done. What must be verified immediately before bump test?

A: 5–10 kPa across a startup strainer is the tripwire here. Anything higher risks cavitation on first rotation. Rotation checks and logic proofs matter, but a blocked suction will damage the pump before those errors show up.

Q: You're troubleshooting and searching "plate heat exchanger sudden pressure drop increase fouling or gasket failure". Symptoms: rising ΔP, declining duty, no external leaks. What's the root cause?

A: A doubling of ΔP with falling U points to flow area loss. Internal bypass from gasket creep usually drops ΔP while losing duty. Deformation and maldistribution show up earlier and often during startup, not gradually.

Q: While checking a vendor calc you search "LMTD correction factor multipass shell and tube calculation". 1–2 exchanger, true countercurrent LMTD = 42 K, correction factor F = 0.85. What effective ΔT do you use?

A: 0.85 is the threshold engineers miss. Effective ΔT is F×LMTD, not the inverse. Using 42 K oversizes duty; dividing by F understates area and fails performance.

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