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Centrifugal Pumps Selection for Oil & Gas

Centrifugal Pumps Selection for Oil & Gas banner
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Centrifugal Pumps Selection for Oil & Gas

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1944 views
Jyoti Swarup
Jyoti Swarup
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  • Session recordings included
  • Certificate of completion

What enrolled engineers say

4 verified reviews
  • May 3, 2026

    Came in needing a cleaner mental picture of how the pump selection stack fits together across upstream oilgas projects, not just another checklist. The section on NPSH margin around the 32‑min mark, where they walk through vapor pressure shifts and show the knock-on effects on impeller trim, stuck with me because it mirrors issues we’ve seen in prod after a feed change. As a TeamLead, I liked how the course ties vendor curves back to arch decisions and infra constraints; it’s easier to align mech choices with ops and obs instead of tossing a PDF over the wall. The API 610 vs ISO callouts were practical, though I wasn't sold on how briefly seal plans were handled, especially for higher RPS cases. This wasn’t academic fluff, and I’ve already pointed a junior to the repo-style worksheets for PR review. mental models like this tend to age better than any single tool rev, which helps when budgets tighten.

    Shuvam R. Verified
  • May 3, 2026

    Section on NPSH margin calc vs vendor curves stuck; it's theory-to-practice for pump selection in oil & gas, wished more on API 610 failure modes.

    Dr Surekha P. · R & D | Drilling & Completion Fluid I Catalysis I Analytical Chemistry I Material Science I LLM Trainer Verified
  • May 3, 2026

    From the first module, the framing stayed close to plant realities rather than textbook curves, which matches how pump choices actually get made under capex and schedule pressure. The section on NPSH margin, especially the worked example comparing vendor curves vs site suction data in Chapter 3, stuck because it mirrors the back-and-forth I’ve had in PRs and vendor calls. It treats selection as a system problem tied to upstream process and downstream control, not just a pump catalog exercise. mostly worked for me, though I wasn’t sold on how briefly minimum flow recycle sizing was handled; a few more numbers would’ve helped. Some of the oil & gas anecdotes lined up with what I see in prod facilities where infra constraints cap RPS before efficiency even matters. The tone stays practical and avoids piling theory onto a topic that already attracts it.

    edward P. · Deputy Director engineering Verified

Is this course for you?

You should take this if

  • You work in Oil & Gas Upstream
  • You're a Mechanical Engineering / Petroleum Technology professional
  • You prefer live, instructor-led training with Q&A

You should skip if

  • You need a different specialisation outside Mechanical Engineering
  • You need fully self-paced, on-demand content

Course details

Course suitable for

Key topics covered

Centrifugal Pumps application for Oil & Gas Industry

Type and descriptions of Pumps and Centrifugal Pumps,

Applicable codes,

Performance Curves,

Affinity laws,

Specific Speed,

NPSH,

Viscosity Corrections

Multi Pump Operations,

Multi stage Centrifugal pumps

Exercise how Centrifugal pumps are to be selected.

API 610 12th ed vs 11th ed.

Codes and Standards List

Opportunities that await you!

Career opportunities

Training details

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

Why people choose EveryEng

Industry-aligned courses, expert training, hands-on learning, recognized certifications, and job opportunities-all in a flexible and supportive environment.

COMPLETED

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Questions and Answers

A: 60 °C is the boundary that catches people. Above roughly 50–60 °C, austenitic grades like 316 become vulnerable to chloride SCC even when oxygen is low and chemistry looks benign. General corrosion of carbon steel is slower here, sulfide mechanisms need H2S, and erosion needs solids that weren't stated.

A: 70% of BEP is the number that matters. Below that, diffuser and impeller recirculation dominate reliability failure modes long before efficiency or MAWP limits show up, and NPSHr behavior is not linear in the way suggested.

A: 100 cP is the cliff. Above that, head and efficiency penalties can exceed 10–20%, shifting BEP enough to invalidate a water-based curve. Diameter and speed tweaks without correction usually push you into off-BEP operation.

A: Plan 11 or 32 failures show up within minutes. Seal faces rely on a few bar of cooled, clean fluid; without it, face temperatures spike and blistering follows long before bearings or hydraulics react.