MaximaLabs
All guides
Reference model (screening)

How to simulate ammonia cracking + h2 purification

Green ammonia is a widely proposed hydrogen *carrier* for shipping — easier to liquefy and transport than liquid H₂ itself, then cracked back to H₂ at the point of use. A fixed-conversion reactor dissociates NH₃ (2 NH₃ → N₂ + 3 H₂, endothermic, 99% conversion at a typical 600 C cracking-furnace outlet) and the cracked gas is polished by an adsorption stage to fuel-cell-grade H₂.

NH3 FEED
Cracker
PSA
H2 Product
TAIL GAS
  1. 1
    Open the ready-made model

    Open the "Ammonia cracking + H2 purification" model in the MaximaLabs workspace — no install, no license. It loads live on the canvas, ready to edit and run.

  2. 2
    Confirm the thermodynamics

    This process is modeled with the PENG-ROBINSON property package over ammonia, n2, h2 — already selected, so the phase equilibrium and enthalpy are physically consistent from the first run.

  3. 3
    Review the flowsheet

    The flowsheet chains Cracker, PSA. Every block is a real, solvable unit op you can reconfigure on the canvas.

  4. 4
    Run the simulation

    Click Run. The deterministic solver converges the material and energy balances (recycles included) and fills the live stream table — the AI never invents a number.

  5. 5
    Read the results and iterate

    Inspect the converged streams, tweak a spec, and re-run — or ask the AI copilot to explain a result or diagnose a failed solve in plain English.

What you'll build
Thermodynamics
PENG-ROBINSON
Components
ammonia, n2, h2
Unit operations
CrackerPSA
Open this model in the workspace

Opens live on the canvas — free, no install.

Explore the model & flowsheet

Modeling assumptions & limitations

What this model captures, and what it deliberately does not — from the engineers who built it.

  1. 1This models the adsorption stage as a single equilibrium Langmuir contact (competitive isotherm, H₂ weakly adsorbed vs. N₂/NH₃ strongly adsorbed) — a real PSA's cyclic pressure-swing/purge steps aren't modeled, only the equilibrium separation a cycle is built around. A true gas-phase membrane stage was left out for the same reason: the solver's `membrane` unit op is a liquid reverse-osmosis model (osmotic-pressure driven), not a gas-permeation membrane, so it doesn't apply here.

Frequently asked questions

What does the Ammonia cracking + H2 purification model simulate?
Green ammonia is a widely proposed hydrogen *carrier* for shipping — easier to liquefy and transport than liquid H₂ itself, then cracked back to H₂ at the point of use. A fixed-conversion reactor dissociates NH₃ (2 NH₃ → N₂ + 3 H₂, endothermic, 99% conversion at a typical 600 C cracking-furnace outlet) and the cracked gas is polished by an adsorption stage to fuel-cell-grade H₂.
Which thermodynamic method does it use?
The PENG-ROBINSON property package, over ammonia, n2, h2 — already selected. You can switch the method on the canvas before running.
Which unit operations are in the flowsheet?
It chains Cracker, PSA. Every block is a real, solvable unit operation you can reconfigure, add to, or remove.
Do I need to install software or buy a license?
No. Ammonia cracking + H2 purification runs entirely in your browser on MaximaLabs — free, no install, no license. Open the model to load it live and run the deterministic solver.

More guides like this

Erlangen, Germany

LOHC hydrogen release (methylcyclohexane dehydrogenation)

A liquid organic hydrogen carrier (LOHC) power train: methylcyclohexane (MCH) is preheated and catalytically dehydrogenated (MCH → toluene + 3H2, endothermic, equilibrium-limited to ~90% single-pass conversion) to release hydrogen for downstream power generation. A flash drum separates the H₂-rich gas from the liquid; a distillation column then recovers the unreacted MCH overhead and recycles it to the reactor feed, closing a real tight liquid recycle loop, while spent toluene leaves the bottoms (to be re-hydrogenated back to MCH off-site, closing the supply-chain loop — out of scope for this dehydrogenation-side flowsheet). Screening-fidelity note: MCH and toluene are genuinely close-boiling (relative volatility ~1.4 under this thermo package at column conditions), so the recycle carries real toluene along with the recovered MCH rather than a sharp cut — a production column would use more stages to purify it further; this shows the recycle topology and its convergence, not an optimized column design.

Direct-reduced-iron (green steel) plant, Boden, Sweden

On-site oxygen: multi-bed vacuum pressure swing adsorption (VPSA)

Medical- / green-steel-grade oxygen generated on site from air by a 4-bed vacuum pressure swing adsorption unit over an N₂-selective zeolite (LiX/13X). This uses the native VPSA unit op — the proven 2-bed Skarstrom engine generalized to N beds with pressure-equalization steps and sub-atmospheric evacuation: nitrogen is adsorbed while oxygen passes as the light product, then each bed is pulled to a vacuum to desorb the nitrogen tail gas. The solver runs the real cyclic transient (tanks-in-series bed discretization + linear-driving-force kinetics + inter-bed equalization) to a periodic steady state — the transient dynamic equilibrium legacy steady-state simulators cannot capture without a separate dynamic license.

Steam-methane-reforming H2 plant, Air Products, Rotterdam, Netherlands

Pressure Swing Adsorption — H2 purification

A 5 bar shift-gas feed (H₂/CO₂, the dominant impurity leaving a steam-methane-reforming shift reactor) is purified across a real cyclic 2-bed PSA unit: while one bed adsorbs CO₂ at high pressure (delivering H₂-rich product), the other regenerates at low pressure, swept countercurrently by a slipstream of that product to desorb CO₂ out the feed end as tail gas — the genuine Skarstrom-cycle mechanism, not a fixed-recovery shortcut. The solver runs the real cyclic transient (tanks-in-series bed discretization + linear-driving-force adsorption kinetics toward the same competitive-Langmuir isotherm uses) to a periodic steady state.

Illustrative flue-gas adsorption capture unit

Flue-gas CO2 capture by solid-sorbent adsorption

A generic solid-sorbent (zeolite-13X-class) adsorption capture step on real combustion flue gas (13 mol% CO₂ — typical of a natural-gas- or coal-fired flue gas, a much higher CO₂ partial pressure than direct-air-capture's ~400 ppm case, which is why this uses the existing Adsorption unit op's real competitive-Langmuir isotherm directly on the flue-gas stream rather than the fixed-recovery separator shortcut the existing DAC examples use). Adsorption-based flue-gas capture is a real, generically licensed technology category (Linde's HISORP CC targets exactly this application); the isotherm parameters here are representative order-of-magnitude values for a zeolite-13X-class sorbent's CO₂/N₂/O₂/H₂O selectivity (real published 13X studies show CO₂ adsorbing roughly an order of magnitude more strongly than N₂/O₂, and water more strongly still, competing for capacity), not pinned to one specific cited paper's exact figures — disclosed as representative, matching MaximaLabs's convention when a precise source isn't confidently pinnable, rather than presenting invented precision. Adsorbent inventory (adsorbent_mass) is sized to a real, honest ~96% CO₂ capture rate — not assumed/rounded to a marketing-friendly number.

Werlte, Germany

CO₂ methanation (e-fuels / power-to-gas)

The Sabatier reaction (CO₂ + 4H₂ ⇌ CH₄ + 2H₂O) converts captured CO₂ and green H₂ into synthetic natural gas at a 97% single-pass-equivalent conversion (real plants stage several adiabatic beds with intercooling to reach this; lumped into one reactor here), then a cooler and knockout drum condense the reaction water from the SNG — the e-fuels loop that closes the loop on captured carbon instead of just storing it.

Herten, Germany

Green hydrogen (electrolysis)

A 1 MW PEM electrolyzer splitting water into hydrogen — a new-energy workflow (carbon footprint + cost track the electricity).

Stop fighting legacy software. Build your first flowsheet in 60 seconds.