Crystallizer Costing Method
Costing Method Parameters
The following parameters are constructed for the unit on the FlowsheetCostingBlock (e.g., m.fs.costing.crystallizer) when applying the cost_crystallizer costing method in the watertap_costing_package:
Description |
Symbol |
Parameter Name |
Default Value |
Units |
|---|---|---|---|---|
Mass-based Capital Costing |
||||
Reference free-on-board (FOB) capital cost \(^1\) |
\(Cost_{ref}\) |
|
675000 |
\(\text{USD}_{2007}\) |
Reference crystallizer capacity \(^1\) |
\(size_{ref}\) |
|
1 |
\(\text{kg/s}\) |
Crystallizer cost exponent parameter \(^1\) |
\(n\) |
|
0.53 |
\(\text{dimensionless}\) |
Installed equipment cost factor \(^2\) |
\(IEC\) |
|
1.43 |
\(\text{dimensionless}\) |
Volume-based Capital Costing |
||||
Capital cost A parameter \(^3\) |
A |
|
16320 |
\(\text{USD}_{2007}\text{/ft}^3\) |
Capital cost B parameter \(^3\) |
B |
|
0.47 |
\(\text{dimensionless}\) |
Operating Costs |
||||
Heating steam pressure \(^4\) |
\(P_{steam}\) |
|
3 |
\(\text{bar}\) |
Heating steam cost parameter \(^5\) |
\(Cost_{steam}\) |
|
0.004 |
\(\text{USD}_{2018}\text{/m}^3\) |
Recirculation pump head height |
\(h_{rec}\) |
|
1 |
\(\text{m}\) |
Recirculation pump efficiency |
\(\eta_{pump}\) |
|
0.7 |
\(\text{dimensionless}\) |
Costing Method Variables
There are no costing method variables unique to the crystallizer.
Capital Cost Calculations
The crystallizer offers two options for computing the capital cost: mass-based costing or volume-based costing.
The mass-based capital cost is dependent upon the mass of solid crystals produced in the crystallizer, \(S\), as shown in the equation below.
\[C_{cap,tot} = IEC * Cost_{ref} * (\frac{S}{size_{ref}})^{n}\]
The volume-based capital cost is dependent upon the unit’s volume, \(V\), as shown in the equation below.
\[C_{cap,tot} = A * V^{B}\]
Operating Cost Calculations
The operating cost of the crystallizer is the sum of the electricity cost for the crystallizer recirculation pump, and the cost of steam for process heating.
\[C_{op,tot} = C_{op,electricity}+C_{op,heat}\]
\(C_{op,electricity}\) is computed with WaterTAP’s standard approach for costing electricity consumption, with assumptions of \(h_{rec}=\) 1m pump head height and \(\eta_{pump}\) = 70% pump efficiency.
Process heat is supplied via steam at \(P_{steam}=\) 3 bar (latent heat), and the process heating cost is computed from the crystallizer heating requirement \(Q\) (\(\text{kJ}\)):
\[C_{op,heat} = Cost_{steam} * \frac{Q}{\rho_{steam} * L_{v}}\]
where \(\rho_{steam}\) and \(L_v\) are the density (\(\text{kg}\text{/m}^3\)) and latent heat of condensation (\(\text{kJ/kg}\)) of steam, respectively.
Code Documentation
References
[1] Woods, Donald R (2007). Rules of Thumb in Engineering Practice. Wiley. 2007. DOI: 10.1002/9783527611119.
[2] Diab, Samir and Gerogiorgis, Dimitrios I (2017). Technoeconomic Evaluation of Multiple Mixed Suspension-Mixed Product Removal (MSMPR) Crystallizer Configurations for Continuous Cyclosporine Crystallization. ACS Organic Process Research & Development, Vol. 21, No. 10 p. 1571-1587. DOI: 10.1021/acs.oprd.7b00225.
[3] Yusuf, A et. al. (2019). CO2 utilization from power plant: A comparative techno-economic assessment of soda ash production and scrubbing by monoethanolamine. Journal of Cleaner Production, Vol. 237, p. 117760. DOI: 10.1016/j.jclepro.2019.117760.
[4] Dutta, B. Principles of mass transfer and separation processes. PHI Learning, 2007.
[5] Panagopoulos, Argyris (2020) Process simulation and techno-economic assessment of a zero liquid discharge/multi-effect desalination/thermal vapor compression (ZLD/MED/TVC) system. International Journal of Energy Research , Vol. 44, No. 1, p. 473-495. DOI: 10.1002/er.4948.