MaximaLabs
Back to gallery
Analytical ultracentrifuge, bioseparations laboratory

Differential sedimentation — Stokes settling, size selectivity, Svedberg — a PENG-ROBINSON process flowsheet

Four centrifuges run side by side on the same medium so the d² law is visible as a result rather than asserted: 20, 50 and 100 nm protein particles at 200,000 × g, plus a 10.24 nm particle at 250,000 × g.

centrifuge is sized by Sigma theory, Σ = Q/(2 v_g), where v_g is the g-amplified Stokes settling velocity v = d²(ρ_p − ρ_m)g/(18η). So the reported sigma_m2 carries the settling velocity, recoverable as v = Q_liquid/(2Σ). Against the closed form the solver agrees to machine precision (relative difference 0 to 4e-16), which makes this a check of the tool and not just a demonstration of it.

What it shows: v(20 nm) = 1.53e-3 cm/s; the 100 nm particle settles exactly 4× faster than the 50 nm one, since velocity goes as the square of diameter and every other term cancels; and the 250,000 × g branch is sized so its velocity is 5e-4 cm/s, giving a sedimentation coefficient s = v/ω²r = 20.4 S — the Svedberg range real proteins occupy (catalase 11.3 S, ribosome ~70 S).

Bounded, and the bound matters. This is terminal Stokes velocity at constant field: no wall, no concentration gradient, no Boycott effect, and no hindered settling. Run the 50 and 100 nm particles for 30 minutes and the arithmetic says they separate by 51 cm, which no rotor can deliver — both pellet against the tube bottom first, the 100 nm one in about four minutes. The ratio is robust; the distance is what the formula says rather than what a centrifuge does.

It is also the reference wiring for a solids flowsheet: the particles arrive as their own phase: "solid" feed with a flat solids payload, wired directly to the centrifuge. Declaring them liquid or mixed, or routing them through a mixer first, leaves the unit with no solid-phase inlet and the solve fails.

207 views 0 forks

LIQ P21
SOL P21
solid
liquor
cake
filt
CF P21
PEL P21
SUP P21
LIQ P22a
SOL P22a
solid
liquor
cake
filt
CF P22a
PEL P22a
SUP P22a
LIQ P22b
SOL P22b
solid
liquor
cake
filt
CF P22b
PEL P22b
SUP P22b
LIQ P23
SOL P23
solid
liquor
cake
filt
CF P23
PEL P23
SUP P23
What this showcases
  • Rigorous PENG-ROBINSON thermodynamics, solved by the same engine every simulation runs on.
  • 1 unit operations modeled: 4× CF P23.
  • Focus areas: Sedimentation, Centrifugation, Stokes law, Svedberg, Bioseparations.
Specification
Thermodynamics
PENG-ROBINSON
Components
water
Unit operations
4× CF P23
Open in workspace

Opens in a new tab, loaded straight into the app — no setup.

Read the step-by-step guide
Python SDK

Reproduce 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("differential-sedimentation-svedberg")
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

Ludwigshafen, Germany

Polymerization reactor comparison: CSTR cascade vs. tubular (PFR)

The same monomer feed, split 50/50 into two trains at equal total reactor volume: a 3-stage CSTR cascade (each stage blending its own new polymer with the MWD already carried by the stream from the stage before it) versus a single tubular (PFR) reactor. Both converge to a real, different Mn/Mw/PDI — the PFR reaches higher conversion at the same total volume, but its cumulative polydispersity is measurably broader than the cascade's, because chain length drifts continuously with conversion along the tube while each CSTR stage makes its own local production under one fixed monomer concentration. See the 'Polymerization Reactors' docs page for the full reasoning.

Amarillo, Texas, USA

Helium liquefaction (Linde-Hampson cycle)

A Joule-Thomson liquefaction loop: helium is compressed, aftercooled, precooled well below its ~40-51 K JT-inversion temperature, then throttled through a valve into a flash drum that draws off liquid helium while the cold vapor recycles back to the compressor suction — the same JT-cycle physics as the platform's LNG/refrigeration loops, run on a fluid whose inversion curve makes precooling mandatory before the throttle can cool it at all.

Brevik, Norway (Heidelberg Materials Norcem — first full-scale cement CCS)

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.

Mont Belvieu NGL fractionation complex, Texas, USA

NGL fractionation: single-shell Petlyuk dividing-wall column

A natural-gas-liquids cut (ethane / propane / n-butane) split into three on-spec products by ONE thermally-coupled dividing-wall column instead of two columns in series. This uses the native Petlyuk unit op: a prefractionator whose reflux and boilup are supplied by the main column (the single condenser + single reboiler), solved by an outer Wegstein loop that converges the bidirectional vapor/liquid coupling to self-consistency — the coupling legacy sequential-modular solvers approximate with two connected columns whose recycle fails to converge.

Pekin, Illinois, USA

Ethanol–water distillation

An 8-stage column concentrating ethanol overhead toward the azeotrope (the headline demo).

Decatur, Illinois, USA

Corn wet milling: starch to high-fructose corn syrup

The sweetener train of a corn wet mill, end to end on the new sugar thermo package. A 35 wt% starch slurry off the mill is saccharified to glucose (glucoamylase, Michaelis-Menten), part-isomerised to fructose, enriched by simulated moving-bed chromatography, and concentrated to syrup in a two-effect evaporator. Three results are worth reading rather than assumed. The isomerase lands at 42% fructose — the real equilibrium of glucose isomerase, which is precisely why an SMB exists downstream: the reaction cannot reach HFCS-55 on its own. The SMB then splits on the cited Ca²⁺-resin affinities (fructose H=0.69 vs glucose H=0.26), sending fructose to the extract and recycling glucose in the raffinate. The evaporator finishes at 77 wt% solids, commercial HFCS syrup spec. That last number is only reachable because of boiling-point elevation. Modelled as inert solids the sugars give no BPE feedback and the evaporator is bimodal — it either does not boil or boils to dry sugar, with nothing in between. The sugar package (Norrish) supplies the real elevation, and syrup concentration becomes a smooth, controllable function of steam (42 → 77 wt% over the sweep range). Starch itself is carried as an involatile pseudo-component: it has no boiling point to characterise, so none is invented.

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