AMP post-combustion CO2 capture (hindered amine) — a ENRTL-AMP process flowsheet
The MEA capture loop run on 2-amino-2-methyl-1-propanol: the same flue gas (12% CO₂ at 1.1 bar), 30 wt% AMP (8 mol%) at a lean loading of 0.10, steam stripping at 1.9 bar and an overhead condenser. AMP is sterically hindered — its carbamate is unstable, so CO₂ goes to bicarbonate and one mole of amine can carry one mole of CO₂ where MEA's carbamate stoichiometry stops at half — and the enrtl-amp package's speciation reproduces that: the rich loading comes out at 0.70 mol/mol against the MEA card's 0.53, so 500 mol/s of solvent does what 650 mol/s of MEA did, with 3.1 MW on the rich heater instead of 3.9. The CO₂ product is 27.7 mol/s at 93 mol%. Same.
Modeling assumptions & limitations
- 1As the MEA card: Kremser stage models, K at the entering liquid, loop open, regeneration to zero loading. The AMP constants are screening-grade (see); the trend against MEA is the physics, the third digit is not.
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- Rigorous ENRTL-AMP thermodynamics, solved by the same engine every simulation runs on.
- 4 unit operations modeled: 2× Strip, Letdown, 2× OVHD COND, Reflux DRUM.
- Focus areas: Carbon capture, AMP, Hindered amine, Electrolyte, Post-combustion.
- Thermodynamics
- ENRTL-AMP
- Components
- n2, co2, o2, water, amp
- Unit operations
- 2× StripLetdown2× OVHD CONDReflux DRUM
Opens in a new tab, loaded straight into the app — no setup.
Read the step-by-step guideReproduce this exact result from Python — the real client.get_example() → run_and_wait() path, not a mockup.
from flowsim.sdk import FlowSimClient
client = FlowSimClient()
example = client.get_example("amp-co2-capture")
sim = client.create_simulation(example["title"], example["flowsheet"])
result = client.run_and_wait(sim["id"])
print(result["status"]) # "converged"
streams = client.streams(sim["id"])Related models
MEA post-combustion CO2 capture (electrolyte NRTL)
The reference amine process on the reference amine: flue gas (12% CO₂ at 1.1 bar, 313 K) scrubbed with 30 wt% aqueous monoethanolamine at a lean loading of 0.20 mol CO₂ per mol MEA, the rich solvent pumped and heated to 388 K, steam-stripped at 1.9 bar, and the overhead condensed at 313 K into a CO₂ product and a reflux-water stream. It runs on the enrtl package — carbamate/bicarbonate/protonation speciation with Davies activity, the CO₂ partial pressure a function of loading and temperature — which is what sets the rich loading of 0.53 mol/mol the absorber reaches and drives the stripper the other way at 390 K. What it computes: 24 mol/s of CO₂ into 695 mol/s of rich solvent, a 39 mol/s CO₂ product at 94 mol% after the condenser knocks out 109 mol/s of water, 3.9 MW of rich-solvent heating for 650 mol/s of circulation (the sensible-heat penalty the sensitivity sweep traces against solvent rate) and 6.8 MW of overhead condensing.
Cement kiln calcination + CO2 liquefaction
Preheated limestone (CaCO₃) enters an indirectly-heated rotary kiln that calcines it toward CaO, releasing a CO₂-rich off-gas; the gas passes a knockout drum, then is compressed and cooled to liquefy the CO₂ for transport/storage.
Post-combustion CO₂ capture
A separator recovers 90% of the CO₂ from a flue-gas stream — the sustainability layer then tracks the captured tonnes.
sCO2 Allam-Fetvedt oxy-combustion power cycle
Natural gas burns in near-pure oxygen, diluted by a large recycled supercritical-CO₂ flow instead of air's nitrogen — the oxy-combustion, near-critical-CO₂ cycle that yields pipeline-ready CO₂ with no separate capture step. Main compressor takes CO₂ from just above its critical point (310 K, 8 MPa vs. Tc=304 K/Pc=7.38 MPa) to 30 MPa; the combined CO2+combustion-product stream expands through a real isentropic-efficiency turbine, still supercritical throughout.
DEA natural-gas sweetening at 50 bar
A high-pressure gas-treating unit on diethanolamine, the canonical secondary amine: 100 mol/s of 5% CO₂ natural gas at 50 bar and 313 K against 200 mol/s of 25 wt% DEA (5.4 mol%), the rich amine let down to 1.8 bar, heated to 388 K and steam stripped, the overhead condensed. The enrtl-dea package carries DEA's cited protonation anchor (pKa 8.9) with a screening-grade carbamate constant. What it computes: a treated gas that is pure methane, a rich loading of 0.52 mol/mol — right at the carbamate ceiling of a secondary amine — a 5.1 mol/s CO₂ product at 89 mol% (the rest methane co-absorbed at 50 bar and water), 1.2 MW on the rich heater. Same model bounds as the MEA card: Kremser stages with the K at the entering liquid, open loop, regeneration to zero loading.
MDEA bulk CO2 removal from shifted syngas
Bulk CO₂ removal ahead of a hydrogen or ammonia unit on N-methyldiethanolamine, the tertiary amine that forms no carbamate and so carries up to one mole of CO₂ per mole as bicarbonate: 200 mol/s of shifted syngas (18% CO₂, 70% H₂) at 30 bar against 450 mol/s of 45 wt% MDEA (11 mol%), regenerated at 1.8 bar with steam. The enrtl-mdea package uses the proton-acceptor speciation only. What it computes: the treated syngas at 85% H₂ / 12% CO with the CO₂ gone, a rich loading of 0.75 mol/mol, a 37 mol/s CO₂ product at 94 mol% and 2.7 MW on the rich heater. Bounds: Kremser stages (the K at the entering liquid, so the absorber captures to completion where a real MDEA absorber is kinetically slow and leaves a slip), open loop, and the loading model caps at 0.99 — the solvent rate is set so the rich end stays well below it, because past the cap the model keeps absorbing.