Catalysis Letters

, Volume 7, Issue 1–4, pp 281–292 | Cite as

Fischer-Tropsch reactor selection

  • Joseph M. FoxIII
Article

Abstract

A comparison of slurry versus fixed-bed reactor design principles for methanol and Fischer-Tropsch distillate production.

Fischer-Tropsch reactor design Fischer-Tropsch fixed bed reactor Fischer-Tropsch fluidized bed (Synthol) reactor slurry reactor methanol production FT distillate production 

Notation

a

gas-liquid interfacial area, m−1

C′Cat

catalyst concentration, kg mole/m3

CHG

hydrogen concentration in gas phase, kg mole/m3

C*HL

hydrogen concentration, liquid, in equilibrium with gas, kg mole/m3

CHL

hydrogen concentration in the liquid phase, kg mole/m3

D

I.D. of reactor, m

GHSV

Gas hourly space velocity, Nm3 (H2 + CO)/[h · m3 reactor volume], (reactor volume is expanded slurry height times cross section area)

H

solubility coefficient of hydrogen =CHG/C*CHL

l

Inlet ratio of CO/H2

kL

liquid side mass transfer coefficient, m/s

kH

effective reaction rate constant for hydrogen consumption, s−1 (note that to agree with space velocity in Nm3/[s · kgCat],kH =kH′ ·C′Cat wherekH′ is in m3/[kg · s]

L

Length of expanded slurry bed, m

P

pressure, kPa

r

rate of hydrogen consumption,r =kH ·CHL, kg moles/[m3 · s]

SV

Space velocity in actual m3 inlet gas/[s · m3]

T

temperature, K

U

Usage ratio of CO/H2

XH

hydrogen fractional conversion per pass (IfU=l,XH =XCO)

α

contraction factor, α = [m3/s(XH2+CO = 1)-m3/s(inlet)]/[m3/s(inlet)]

α*

contraction factor modified for H2 conversion, α* = α · (1 +U)/(1 +l)

εL

fractional liquid hold-up

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References

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Copyright information

© J.C. Baltzer A.G., Scientific Publishing Company 1991

Authors and Affiliations

  • Joseph M. FoxIII
    • 1
  1. 1.Bechtel Group Inc.San FranciscoUSA

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