How to simulate monoclonal antibody — perfusion culture to freeze-dried vial

A monoclonal antibody from the perfusion culture that makes it to the freeze-dried vial: **culture → capture → viral inactivation → virus filtration → UF/DF → lyophilization**. Every downstream step was a standalone calculator before this; wiring them together is what makes the train's numbers agree with each other — raise the culture's productivity and the capture column, the filter area and the vial count all move with it. **The protein enters as a product, not a feed.** No property databank carries a 148 kDa antibody (a biomolecule databank is a licensed-data gap, not a missing formula), so the mAb is produced by the bioreactor rather than declared on a feed — a feed component has to be priced thermodynamically, and this one cannot be. **Capture (`PROTEIN_A`).** Sized on **dynamic binding capacity** via Bohart-Adams, the model derived for the near-irreversible isotherm a Protein A resin has — the rigorous bed PDE does not converge at a ~1e-3 g/L dissociation constant, so the method here is the one process development actually uses. Titre and harvest volume come from the feed stream, so changing the upstream titre resizes the column. **Viral inactivation (`LOW_PH_HOLD`).** The kill is **biphasic**: the resistant fraction imposes a hard −log₁₀(f) ceiling, so a longer hold stops helping. single-population fit would promise unlimited kill and justify a hold that cannot deliver — raise `target_log_reduction` past the ceiling and the step says so instead of reporting a number. **Virus filtration (`VIRUS_FILTER`).** Sized on **capacity**, not flux: the filter plugs, so throughput climbs toward Vmax and never past it. That is why more pressure does not rescue an undersized filter, and why the step reports throughput against capacity. **UF/DF (`UFDF`).** Film-theory polarization and the virial osmotic-pressure flux equation solved *together* — which is what produces the pressure-independent plateau that defines ultrafiltration. Raise the TMP and watch the flux barely move while the wall concentration climbs; raise the mass-transfer coefficient (crossflow) instead and it responds. The reverse-osmosis `membrane` op structurally cannot show that. **Freeze drying (`LYO`).** Primary drying by the Pikal vial model, with the **collapse margin** the cycle actually has to respect. Push the shelf temperature up and the cycle shortens right up until the product crosses its collapse temperature and the batch is lost. **No biologics data ships, deliberately.** Every number that decides an answer here — resin capacity and rate constant, the virus kill rate and Vmax, the protein's second virial coefficient, the vial heat-transfer coefficient and cake resistance — is measured for *your* molecule, *your* resin, *your* dryer. The values in this example are illustrative and each step refuses rather than defaulting when one is missing. **Bounds.** Screening-grade process development, not a tech-transfer package: pH elution is a declared yield rather than a desorption model, the ICH Q5A clearance budget across steps lives in the Viral clearance tool (a budget spans steps), and no GMP artefacts — batch records, 21 CFR Part 11 — exist here.

Frequently asked questions

What does the Monoclonal antibody — perfusion culture to freeze-dried vial model simulate?

A monoclonal antibody from the perfusion culture that makes it to the freeze-dried vial: **culture → capture → viral inactivation → virus filtration → UF/DF → lyophilization**. Every downstream step was a standalone calculator before this; wiring them together is what makes the train's numbers agree with each other — raise the culture's productivity and the capture column, the filter area and the vial count all move with it. **The protein enters as a product, not a feed.** No property databank carries a 148 kDa antibody (a biomolecule databank is a licensed-data gap, not a missing formula), so the mAb is produced by the bioreactor rather than declared on a feed — a feed component has to be priced thermodynamically, and this one cannot be. **Capture (`PROTEIN_A`).** Sized on **dynamic binding capacity** via Bohart-Adams, the model derived for the near-irreversible isotherm a Protein A resin has — the rigorous bed PDE does not converge at a ~1e-3 g/L dissociation constant, so the method here is the one process development actually uses. Titre and harvest volume come from the feed stream, so changing the upstream titre resizes the column. **Viral inactivation (`LOW_PH_HOLD`).** The kill is **biphasic**: the resistant fraction imposes a hard −log₁₀(f) ceiling, so a longer hold stops helping. single-population fit would promise unlimited kill and justify a hold that cannot deliver — raise `target_log_reduction` past the ceiling and the step says so instead of reporting a number. **Virus filtration (`VIRUS_FILTER`).** Sized on **capacity**, not flux: the filter plugs, so throughput climbs toward Vmax and never past it. That is why more pressure does not rescue an undersized filter, and why the step reports throughput against capacity. **UF/DF (`UFDF`).** Film-theory polarization and the virial osmotic-pressure flux equation solved *together* — which is what produces the pressure-independent plateau that defines ultrafiltration. Raise the TMP and watch the flux barely move while the wall concentration climbs; raise the mass-transfer coefficient (crossflow) instead and it responds. The reverse-osmosis `membrane` op structurally cannot show that. **Freeze drying (`LYO`).** Primary drying by the Pikal vial model, with the **collapse margin** the cycle actually has to respect. Push the shelf temperature up and the cycle shortens right up until the product crosses its collapse temperature and the batch is lost. **No biologics data ships, deliberately.** Every number that decides an answer here — resin capacity and rate constant, the virus kill rate and Vmax, the protein's second virial coefficient, the vial heat-transfer coefficient and cake resistance — is measured for *your* molecule, *your* resin, *your* dryer. The values in this example are illustrative and each step refuses rather than defaulting when one is missing. **Bounds.** Screening-grade process development, not a tech-transfer package: pH elution is a declared yield rather than a desorption model, the ICH Q5A clearance budget across steps lives in the Viral clearance tool (a budget spans steps), and no GMP artefacts — batch records, 21 CFR Part 11 — exist here.

Which thermodynamic method does it use?

The NRTL property package, over ethanol, water — already selected. You can switch the method on the canvas before running.

Which unit operations are in the flowsheet?

It chains PERF, Protein A, LOW PH HOLD, Virus Filter, UFDF, LYO. 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. Monoclonal antibody — perfusion culture to freeze-dried vial runs entirely in your browser on MaximaLabs — free, no install, no license. Open the model to load it live and run the deterministic solver.