Chemical Process Design
Chemical Process Design Chemical Process Design
3.- COST ESTIMATION OF EQUIPMENT Guthrie´s modular method to preliminary design. Updated Bare Module Cost = UF . BC . (MPF + MF -1) BC Williams Law: C = BC =Co (S/So) α Non-linear behaviour of Cost, C vs., Size, S Economy of Scale (incremental cost decrease with larger capacities Tables for each equipment C = BC =Co (S/So) α log C = log (Co/So) α + α log S Co, So. Parameters of Basic configuration Costs and Capacities α. α. Parameter < 1 economy of scale Base Cost for Pressure Vessels: Vertical, horizontal, tray stack C =Co (L/Lo) a (D/Do) b Base Cost for Process Equipment C =Co (S/So) α ; Range of S 28
MF: Module Factor, affected by BC, taking into account labor, piping instruments, accessories, etc. MF 2 : < 200.000 $ MF 4 : 200.000 - 400.000 $ MF 6 : 400.000 - 600.000 $ MF 8 : 600.000 - 800.000 $ MF 10 : 800.000 - 1.000.000 $ MPF: Materials and Pressure correction Factors Φ Φ (Fd, Fm, Fp, Fo, Ft) Empirical factors that modified BC and evaluate particular instances of equipment beyond a basic configuration: Uninstalled Cost = (BC x MPF) Fd: Design variation Fm: Construction material variation Fp: Pressure variation Fo: Operating Limits ( Φ of T, P) Ft: Mechanical refrigeration factor (Φ Φ T evaporator) UF: Update Factor, to account for inflation. UF = Present Cost Index (CI actual ) / Base Cost Index (CI base ) CI: Chemical Engineering Plant Cost Index (www.che.com) YEAR CI YEAR CI 1957-59 100 1996 382 1968 115 (Guthrie paper) 1997 386.5 1970 126 1998 389.5 1983 316 2003 402 1993 359 2009 539.6 1995 381 2010 532.9 29
- Page 1 and 2: Chemical Process Design Subj
- Page 3 and 4: 1.- INTRODUCTION Process Alternativ
- Page 5 and 6: Cost Estimation Method of Guthrie
- Page 7 and 8: An example of Cost Estimation Equip
- Page 9 and 10: SHORTCUTS for VESSEL SIZING (Flash
- Page 11 and 12: SHORT CUT for REACTORS SIZING First
- Page 13 and 14: Heat exchanger: Countercurrent, ste
- Page 15 and 16: HEAT EXCHANGERS 15
- Page 17 and 18: SHORT CUT for DISTILLATION COLUMS S
- Page 19 and 20: DISTILLATION COLUMNS 19
- Page 21 and 22: SHORT CUT for COMPRESSORS (or TURBI
- Page 23 and 24: Centrifugal pumps selection guide.
- Page 25 and 26: Guthrie Material and Pressure Facto
- Page 27: 3.- COST ESTIMATION OF EQUIPMENT: B
3.- COST ESTIMATION OF EQUIPMENT<br />
Guthrie´s modular method to preliminary design.<br />
Updated Bare Module Cost = UF . BC . (MPF + MF -1)<br />
BC<br />
Williams Law: C = BC =Co (S/So) α<br />
Non-linear behaviour of Cost, C vs., Size, S Economy of Scale (incremental<br />
cost decrease with larger capacities<br />
Tables for each equipment<br />
C = BC =Co (S/So) α log C = log (Co/So) α + α log S<br />
Co, So. Parameters of Basic configuration Costs and Capacities<br />
α. α. Parameter < 1 economy of scale<br />
Base Cost for Pressure Vessels: Vertical, horizontal, tray stack<br />
C =Co (L/Lo) a (D/Do) b<br />
Base Cost for <strong>Process</strong> Equipment<br />
C =Co (S/So) α ; Range of S<br />
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