You're mid-turnaround on a 1999 SMR revamp and the spec calls up API 560 for the reformer firebox. The contract is silent on revision year, and the OEM GA references flame arrestors sized per an older edition. You're searching "API 560 latest edition applies to brownfield contract". What governs whether the superseded or current API 560 requirement applies?

The hard boundary is contract award. API standards aren’t retroactive unless the contract drags them forward with a ‘latest edition’ clause. Without that language, you’re tied to what was enforceable when the EPC took risk, even if the newer API 560 tightened flame geometry or minimum clearances.

An SMR high-temperature shift reactor shows rising ΔP from 0.18 to 0.42 bar over three months, while CO slip at the outlet increases from 0.6% to 1.1%. Feed sulfur is nominally <50 ppb. You're googling "HT shift reactor pressure drop increase CO slip" during the night shift. What failure mode best fits both symptoms?

The number that matters is the doubling of ΔP alongside higher CO. Sulfur kills activity but doesn’t choke flow. Attrition raises ΔP but usually improves apparent conversion early. Carbon fouling does both at once by blocking pores and shifting equilibrium away from H₂.

A PEM electrolyzer skid relies on high-integrity pressure protection (HIPPS) to isolate the stack at 35 bar(g). The downstream dryer relief valve is sized for blocked outlet. During a control fault, HIPPS fails to close. You're searching "PEM electrolyzer HIPPS failure consequence". What physical consequence is NOT prevented by the relief valve alone?

The threshold is membrane ΔP, not vessel MAWP. Relief valves protect steel. They don’t limit the transient pressure differential across a PEM stack, where even a few bar can tear the membrane before any PSV reacts.

During SMR load reduction from 100% to 70%, the steam-to-carbon ratio drifts from 3.2 to 2.4 mol/mol due to a sticking FCV. Reformate methane slip rises. You're typing "SMR low steam to carbon response". What’s the correct operator response to stabilize hydrogen yield?

2.5 mol/mol is the red line. Below that, carbon risk dominates. More heat accelerates coke. The only move that arrests damage while you fix the valve is to back off feed and get steam back into ratio.

An alkaline electrolyzer consumes 52 kWh/kg H₂ on an LHV basis. Plant load is 8,000 kg/day. You're searching "alkaline electrolyzer power consumption calculation" to sanity-check the transformer size. What continuous electrical power is required, ignoring auxiliaries?

The trap is day-to-hour conversion. 8,000 kg/day at 52 kWh/kg equals 416,000 kWh/day. Divide by 24 and you land at about 17.3 MW, before rectifier and compression losses.

A hydrogen product stream feeds fuel cells requiring ISO 14687 purity. The legacy spec allows 0.5 ppm CO. You're checking "ISO 14687 hydrogen CO limit fuel cell" while reviewing a PSA upgrade. Which requirement drives the tighter CO limit?

The hard number is 0.2 ppm CO. That limit exists because platinum anodes lose activity fast. It’s not about steel or adsorption; it’s electrochemistry at the cell face.

A PSA unit for SMR hydrogen shows declining recovery from 78% to 70%, while product purity stays at 99.97%. Tail gas flow increases. You're searching "PSA hydrogen low recovery high purity" during troubleshooting. What’s the most likely cause?

The boundary is purity holding steady. Aging adsorbent holds less hydrogen per cycle, so you dump more to tail gas. Leaks and low feed pressure usually hit purity first.

An ATR operates at 28 bar with oxygen injection from a cryogenic ASU. The O₂ flow interlock tied to methane flow fails open. You're searching "ATR oxygen methane interlock failure consequence" for a HAZOP closeout. What immediate hazard results?

The critical limit is local O₂/CH₄ ratio. Without the interlock, you create hot spots well above design flame temperature. That attacks refractory fast, long before product specs shift.

A PEM electrolyzer stack operates at 1.8 A/cm² with an active area of 1.2 m² per cell and 400 cells. You're searching "PEM electrolyzer stack current calculation" to size DC bus bars. What total current does the rectifier need to deliver?

The unit trap is cm² to m². 1.8 A/cm² equals 18,000 A/m². Multiply by 1.2 m² and then by 400 cells wired in parallel on the DC side, and you land at roughly 86 kA.

A low-temperature shift reactor inlet temperature drifts up from 200 °C to 240 °C due to a bypass valve leak. CO conversion drops. You're googling "LT shift high inlet temperature effect" before calling operations. What adjustment actually recovers performance?

The number is 200 °C. LT shift is equilibrium-limited above that. Slowing the gas buys conversion back. More heat just pushes equilibrium the wrong way.

Hydrogen Energy: Production

Hydrogen Energy: Production

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Duration 896 Min

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Properties of Hydrogen

30 Lectures

896 min

Properties of Hydrogen
23 min
Status of Hydrogen
9 min
Methods of Hydrogen Production
25 min
Steam methane reforming part -1
28 min
Steam methane reforming Part-2
42 min
Steam reforming of higher hydrocarbons
0 min
Tutorial 1
27 min
Advanced methods of steam reforming
39 min
Partial oxidation method for Hydrogen production
32 min
Autothermal Reforming
32 min
Combined dry, bi and tri reforming
30 min
Reforming using alternate energy sources
33 min
Tutorial 2
33 min
Hydrogen production by methane decomposition
36 min
Hydrogen production from Biomass part-1
28 min
Hydrogen production from Biomass Part-2
34 min
Hydrogen production from biomass- Part 3
25 min
Hydrogen production from coal
28 min
Tutorial 3
41 min
Hydrogen separation and purification Part-1
37 min
Hydrogen separation and purification part-2
30 min
Thermochemical cycles for hydrogen production
36 min
Electrolysis of water for hydrogen production
38 min
Fundamentals of electrolysis of water
25 min
Electrolytic cell components and electrolyzer stack
31 min
Different types of electrolyzer technologies
32 min
Photoelectrochemical hydrogen production
16 min
Tutorial 4
43 min
Technical Comparison of Various Hydrogen Production Routes
21 min
Economics and Status of Various Hydrogen Production Routes
42 min

Status of Hydrogen supply and demand

0 Lectures

0 min

Course details

Course suitable for

Energy & Utilities
Oil & Gas
Pharmaceutical & Healthcare
Chemical & Process
Petroleum

Key topics covered

Hydrogen Energy: Production

Properties of Hydrogen
Status of Hydrogen
Methods of Hydrogen Production
Steam methane reforming part -1 and 2
Steam reforming of higher hydrocarbons
Advanced methods of steam reforming
Partial oxidation method for Hydrogen production
Autothermal Reforming
Combined dry, bi and tri reforming
Reforming using alternate energy sources
Hydrogen production by methane decomposition
Hydrogen production from Biomass part-1, 2, 3
Hydrogen production from coal
Hydrogen separation and purification Part-1, 2
Thermochemical cycles for hydrogen production
Electrolysis of water for hydrogen production
Fundamentals of electrolysis of water
Electrolytic cell components and electrolyzer stack
Different types of electrolyzer technologies
Photoelectrochemical hydrogen production
Technical Comparison of Various Hydrogen Production Routes
Economics and Status of Various Hydrogen Production Routes
Tutorials 1,2, 3, 4

FREE

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