Hopper

Published on June 2016 | Categories: Documents | Downloads: 131 | Comments: 0 | Views: 1606
of 59
Download PDF   Embed   Report

Comments

Content


MULTI-PHASE AND CATALYTIC CHEMICAL
REACTORS DESIGN SIMULATION TOOL
Jack R. Hopper
Jamal M. Saleh
Sandeep Waghchoure
Sandesh C. Hegde
Niraj Ramachandran
Lamar University, Beaumont, TX 77710


Ralph W. Pike
Louisiana State University
Baton Rouge, LA 70803

Overview of Advanced Process Analysis System
Process control
Process Modification
Advanced Process Analysis System
On-Line Optimization
Flowsheet Simulation
Reactor Analysis Pinch Analysis Pollution Index
OBJECTIVE

To develop a User Friendly Simulation Package for multi-
phase catalytic and non-catalytic reactor analysis as a
component for the Advanced On-line Process Analysis
System for Pollution Prevention
REACAT REACTOR SIMULATION TOOL
FEATURES
 User Friendly input/ output interface
 Graphical and Tabular Data Output
 Extensive Selection of Reactor Models
 Component Material Balances for Gas, Liquid and
Catalyst Phase
 Total Energy Balance
 Prediction of reactor hydrodynamics such as
pressure drop, power consumption, catalyst wetting
factor and flow regimes
 Reactor Models with numerous Options
Classification of Homogeneous and Heterogeneous
Reactor Models
REACTION PHASE REACTOR MODEL
Homogeneous Plug Flow, CSTR, Batch
Heterogeneous:-
Catalytic
Two Phase
Gas-Catalyst or
Liquid-Catalyst
Three Phase
Gas-Liquid-Catalyst
Non-Catalytic
Gas-Liquid
Packed-Bed or Fluidized-Bed
Trickle-bed, Bubble Fixed-Bed
CSTR Slurry, Bubble Slurry,
3-Phase Fluidized
Gas-Liquid CSTR, Gas-Liquid
Bubble Column
Reactor Definitions
•Catalytic Packed Bed: Gas or Liquid Reactants flow over a fixed bed of
catalysts.

•Catalytic Fluidized Bed: The up-flow gas or liquid phase suspends the fine
catalyst particles.

•CSTR Gas-Liquid: Liquid and gas phases are mechanically agitated

•Bubble Gas-Liquid Bed: Liquid phase is agitated by the bubble rise of the
gas phase. Liquid phase is continuous.
Reactor Definitions (Contd..)
•Trickle-Bed: Concurrent down-flow of gas and liquid over a fixed-bed of
catalyst. Liquid trickles down, while gas phase is continuous

•Bubble-Fixed Bed: Concurrent up-flow of gas and liquid. Catalyst bed is
completely immersed in a continuous liquid flow while gas rises as
bubbles.

•CSTR Slurry: Mechanically agitated gas-liquid-catalyst reactor. The Fine
catalyst particles are suspended in the liquid phase by means of agitation.
(Batch liquid phase may also be used)

•Bubble Slurry Column: Liquid is agitated by means of the dispersed gas
bubbles. Gas bubble provides the momentum to suspend the catalyst
particles.

•Three-Phase Fluidized Bed: Catalyst particles are fluidized by an
upward liquid flow while gas phase rises in a dispersed bubble regime.
Reactor Types Included in the Reactor Simulation
Tool, ReaCat
Plug Flow
CSTR
Batch
Homogeneous Reactors:
Reactor Types Included in the Reactor Simulation Tool,
ReaCat (Contd..)
Gas /Liquid
Catalytic Reactors
Fixed Bed
Fluidized
Bed
Gas-Liquid Reactors
Gas
Liquid
Gas-Liquid
CSTR
Liquid
Gas
Gas-
Liquid
Bubble
Column
Two-Phase Reactors:
Reactor Types Included in the Reactor Simulation Tool,
ReaCat (Contd..)
Three-Phase Reactors:
Three Phase Catalytic Reactors
Liquid
Liquid
Liquid Liquid
Gas
Gas
Gas
Gas
Gas
Liquid
Cocurrent
Downflow Trickle
Bed
Cocurrent
Upflow Packed
Bed
Bubble Slurry
Column
Three-Phase Fluidized
Column
Gas-Liquid Catalytic CSTR
Slurry Reactor
REACTION RATE MODEL OPTIONS
Power-law reaction rate or Langmuir- Hinshelwood model to
account for the adsorption effects.

Correlations to estimate the external mass transfer effects
and dispersion coefficients

Catalytic effectiveness factor estimation to account for intra-
particle resistance

Flow Regime Options

Isothermal and non-isothermal/non-adiabatic conditions

Multi-reaction systems with up to 30 reactions and 36
components
Industrial Examples of Multi-phase and Catalytic
Reactors
Catalytic Gas/ Liquid Fluidized-bed Reactor
• Fluid Catalytic Cracking
• Production of Allyl Chloride.
• Production of Phthalic Anhydride
• Acrilonitrile by the Sohio Process



Catalytic Fixed Bed Reactor
• Partial oxidation of O-xylene to Pthalic Anhydride
• Hydrogenation of Aromatics and Olefins
• Dehydrogenation of Ethylbenzene to Styrene

Industrial Examples of Multi-phase and Catalytic
Reactors
Three-phase Reactor:

Trickle-Bed
-Catalytic hydro-desulfurization
-Catalytic hydrogenation
-Catalytic hydrocracking
Fixed-bed upward bubble-flow
-Fischer-Tropsch
-Coal liquefaction
CSTR Slurry
-Hydrogenation of fatty oils and unsaturated fats.
-Hydrogenation of acetone
Bubble-Slurry Column
-Catalytic oxidation of olefin
-Liquid-phase xylene isomerization
Three-phase fluidized Bed
-Production of calcium acid sulfite
-Coal liquefaction, SRC process

Industrial Examples of Multi-phase and Catalytic
Reactors
Gas-Liquid Continuous Stirred Tank Reactor:

- Oxidation of cyclohexane to adipic acid, cumene to cumene
hydroperoxide, and toluene to benzoic acid.

- Absorption of SO
3
in H
2
SO
4
for manufacture of Oleum

- Absorption of NO
2
in water for the production of HNO
3

-

Addition of HBr to alpha olefins for the manufacture of alkyl
bromide.

- Addition of HCl to vinyl acetylene for the manufacture of
chlroprene.

- Absorption of butenes in sulfuric acid for conversion to
secondary butanol.

Multi-phase Reactors- Advantages and
Disadvantages
Advantages Disadvantages
Catalytic Fixed
Bed Reactor
+
The fluid flow regimes
approach plug flow, so
high conversion can be
achieved.
+
Pressure drop is low.
+
Owing to the high hold-
up there is better radial
mixing and channeling
is not encountered.
+
High catalyst load per
unit of reactor volume
+
The intra-particle
diffusion
resistance is very
high.
+
Comparatively low
Heat and mass
transfer rates
+
Catalyst
replacement is
relatively hard and
requires shut
down.
Multi-phase Reactors- Advantages and
Disadvantages
Advantages Disadvantages
Catalytic
Fluidized-bed
Reactor
+
The smooth, liquid-like flow of particles
allows continuous controlled operations
with ease of handling.
+
Near isothermal conditions due to the rapid
mixing of solids.
+
Small Intra-Particle resistance leads to a
better heat and mass transfer rate.
+
This violent particle motion of
particles tends to homogenize all
intensive properties of the bed.
Thus it is not generally possible to
provide an axial temperature
gradient which might be highly
desirable in some instances.
+
Erosion by abrasion of
particles can be serious.
+
Particle attrition
Three-phase Reactors- Advantages and
Disadvantages
Advantages Disadvantages
Trickle-
Bed
Reactor
+
Gas and liquid flow regimes
approach plug flow; high
conversion may be achieved.
+
Large catalyst particle, therefore,
catalyst separation is easy.
+
Low liquid holdup, therefore liquid
homogenous reactions are
minimized.
+
Low pressure drop
+
Flooding problems are not
encountered.
+
High catalyst load per unit reactor
volume.
+
Poor distribution of the
liquid-phase
+
Partial wetting of the catalyst
+
High intra-particle resistance
+
Poor radial mixing
+
Temperature control is
difficult for highly exothermic
reactions
+
Low gas-liquid interaction
decreases mass transfer
coefficients.
Three -phase Reactors- Advantages and
Disadvantages
Advantages Disadvantages
Bubble
Fixed- Bed
Reactor
+
High liquid holdup,
therefore, catalyst are
completely wetted, better
temperature control, and no
channeling problems.
+
Gas-liquid mass transfer is
higher than in Trickle bed
due to higher gas-liquid
interaction.
+
Axial back mixing is
higher than trickle-
beds, conversion is
lower.
+
Feasibility of liquid side
homogeneous
reactions
+
Pressure drop is high
+
Flooding problems may
occur.
Three -phase Reactors- Advantages and
Disadvantages
Advantages Disadvantages
Slurry and
3-phase Fluidized
Reactor
+
Ease of heat
recovery and
temperature
control.
+
Ease of catalyst
supply and
regeneration
process.
+
Low intra-particle
resistance.
+
High external
Mass transfer rate
(Gas-liquid and
Liquid Solid)
+
Axial mixing is
very high
+
Catalyst
separation may
require filtration.
+
High liquid to solid
ratio may promote
liquid side
reactions.
+
Low catalyst load.
Multi-phase Reactors- Advantages and
Disadvantages
Advantages Disadvantages
Gas Liquid
Continuous
Stirred
Tank
Reactor
+
Very effective for viscous
liquids and at very low gas
rates and large liquid volumes.
+
Best for system with large
heat effects because of
superior heat transfer
characteristics.
+
Useful for slow reactions
requiring high liquid holdup.
+
Residence time of liquid and
extent of agitation can be
easily varied.
+
Both liquid and gas phase
are almost completely
backmixed.
+
High power consumption per
unit volume of the fluid.
+
Sealing and stability of Shaft
in tall reactors.
Comparison of Three Phase Trickle- Bed and
Bubble Fixed Bed Reactors
Characteristics Trickle- Beds Bubble Fixed-
Beds
Pressure Drop Channeling at low liquid
flow rates
No Liquid flow
maldistribution
Heat Control Relatively Difficult Easy
Radial mixing Poor radial mixing Good mixing
Liquid/Solid ratio Low High
Catalyst Wetting Partial wetting is possible Complete
wetting
Conversion High Poor due to
back mixing
Comparison of Three Phase Suspended Bed
Reactors
Characteristic CSTR Slurry Bubble Slurry Three- phase
Fluidized
Catalyst Attrition Significant Insignificant Insignificant
Mass and Heat
Transfer
Efficiencies
Highest High High
Mechanical
Design
Difficult Simple Simple
Catalyst
Separation
Easy Easy Easiest
Power
Consumption
Highest Intermediate Lowest
Catalyst
Distribution
Uniform Nonuniformity
may exist
Nonuniformity
may exist
Gas-Liquid-Solid Contact in Three-phase Reactors
External
Diffusion
Internal
Diffusion
Catalytic Surface
Bubble Particle
Theory of Catalytic Gas- Liquid Reactions


A
(G)
+ B
(L)
C

Gaseous reactant A reacts with non-volatile liquid reactant B on
solid catalyst sites.

Mechanism Of Three- Phase Reactions:-
Mass Transfer of component A from bulk gas to gas-liquid
interface
Mass transfer of component A from gas-liquid interface to bulk
liquid
Mass transfer of A& B from bulk liquid to catalyst surface
Intraparticle diffusion of species A& B through the catalyst pores
to active sites.
Adsorption of both or one of the reactant species on catalyst
active sites
Surface reaction involving at least one or both of the adsorbed
species
Desorption of products, reverse of forward steps .

Common Flow Regimes in Industrial Catalytic
Gas- Liquid Reactors
Catalytic Gas-Liquid Reactor Common Flow Regime
Cocurrent Down-Flow Fixed-
Bed
Trickle-Flow
Cocurrent Up- Flow Fixed-Bed Bubble- Flow
Bubble Column Slurry Reactor Homogeneous Bubble- Flow
Three- phase Fluidized- Bed Bubble- Flow
Design Models For Catalytic Gas- Liquid Reactors
Flow Regime Gas-phase
Design Model
Liquid- Phase
Design- Model
Trickle Flow
Cocurrent
Down-Flow Fixed-Bed
Dispersion Dispersion
CSTR Slurry, Continuous or Semi-
Batch
CSTR CSTR/ Batch
Homogeneous Bubble- Flow Continuous
Bubble Column
Slurry Reactor
Dispersion Dispersion
Homogeneous Bubble- Flow Semi-
Batch Bubble Column Slurry
Dispersion Batch
Bubble Flow
Three- phase Fluidized Bed
Dispersion Dispersion
Correlations Used for the Three-Phase Catalytic Reactors
Correlation Trickle-Bed Fixed Up-Flow CSTR Slurry Bubble Slurry 3-Phase
Fluidized
Pressure drop Larkins et al.
1961
Ellman et al.
1988
Turpin &
Hintington 1967 - - -
L & G Holdup Sato et al. 1973
Ellman et al.
1989
Fukushima &
Kuasaka 1979
Achwal &
Stepanek 1976
Galderbank
1958
Yung et al.
1979
Yamashita &
Inoue 1975
Maselkar 1970
Kim et al.
1975
L-S Mass
Trans. Coeff.
Van Krevelen
1948
Dharwadker &
Sylvester 1977
Specchia et al.
1978
Sano et al.
1947
Kobayashi &
Saito 1965
Lee et. Al
1974
L Dispersion
Coeff.
Michell &
Furzer 1972
Stiegel & Shah
1977 -
Deckwer et
al.1974
El-Temtamy
1979
G Dispersion
Coeff.
Hochman &
Effron 1969 - -
Mangartz &
Pilhofer 1981 -
Wall Heat
Transf. Coeff.
Baldi 1979
- -
Fair 1967
-
Power
Consumption - -
Luong &
Volesky 1979
Michel and
Miller 1962
- -
Correlations Used for the 2-Phase Reactors
Gas Liquid Continuous Stirred Tank Reactor

1. Maximum Gas Flow rate (Q
Gmax
) – Zwietering (1963)
2. Bubble diameter (d
b
) – Van Dierendonck (1970)
3. Gas holdup (c
G
) - Van Dierendonck (1970)
4. Liquid side Mass transfer coefficient (k
L
) – Van Dierendonck (1970)
5. Liquid side Mass transfer coefficient (k
L
) for single bubbles - Hughmark(1971)

Catalytic Liquid Fluidized Bed

Mass Transfer Coefficient (K
L
) – Chu, Kalil and Wetteroth (1953)

Catalytic Gas Fluidized bed

1. Voidage at Minimum Fluidization (c
mf
) – Broadhurst and Becker (1975)
2. Velocity at Minimum fluidization (U
mf
) – Kunii and Levenspiel (1969 )
3. Bubble Diameter (D
B
)- Horio and Nonaka (1984)
4. Mass Transfer Coefficients (K
BC
and K
CE
) – Kunni and Levenspiel (1969)
5. Coefficient for Axial Dispersion (D
GA
) – Yoshida,Kunii and Levenspiel(1969)

Calculation of Catalytic Effectiveness Factor
Catalytic Effectiveness Factor:


where
|- Thiele Modulus

1
st
order reaction rate:

Spherical Pellet

Cylindrical Pellet

Slab Pellet



)
3
1
3 (
1
|
|
|
q ÷ = Coth
De p kSa
R
/
3
µ | =
De p kSa
R
/
2
µ | =
De p kSa L / µ | =
Catalytic Fixed-Bed Reactor - Design Model
Mass Balance around the catalyst

Gas-Phase component mass balance (Plug Flow model)


Gas-Phase component mass balance (Dispersion model)


Energy Model

i net S G i c c R i C C a k ) ( ) ( ) ( ÷ = ÷ q
0 . 0 ) ( ) ( = ÷ ÷ ÷ i S G i c c
Gi
G C C a k
dz
dC
U
0 . 0 ) ( ) (
2
2
= ÷ ÷ ÷ i S G i c c
Gi
G
Gi
G C C a k
dz
dC
U
z d
C d
i D
) ( ) ( Ta T UA j H Rj
dz
dT
Cp U R G G G ÷ + A =
¿
µ
Catalytic Gas-Fluidized Bed Reactor- Design Model
Bulk Gas Phase( Bubble Phase):
Plug Flow:-



With Axial Dispersion:



Intermediate(Cloud- Wake) Phase:


Catalyst (Emulsion) Phase:


Energy Balance:

) (
ic ib BC
ib
b
C C K
dZ
dC
U ÷ = ÷
) (
2
2
ic ib BC
ib
b
ib
ga
C C K
dZ
dC
U
dZ
C d
D ÷ = ÷
) ( ) ( ) (
ie ic CE e iCloudPhas c ic ib BC
C C K R C C K ÷ + = ÷ _
hase iEmulsionP e ie ic CE
R C C K ) ( ) ( _ = ÷
) ( * *
Re
1
actor ambient j
NR
j
pg b g
T T a U Hr Rj
dZ
dT
C U ÷ + A =
¿
=
µ
Catalytic Liquid -Fluidized Bed Reactor-Design Model
Liquid-phase component balance:

Plug Flow:-
(1)


Dispersion:-
(2)


Catalyst (Emulsion) Phase:
(3)


Energy Balance:-
(4)




) (
iS iL L
iL
L
C C K
dZ
dC
U ÷ = ÷
) (
2
2
iS iL L
iL
L
iL
La
C C K
dZ
dC
U
dZ
C d
D ÷ = ÷
hase iCatalystP iS iL L
R C C K ) ( ) ( = ÷
) ( * *
Re
1
actor ambient j
NR
j
pL L L
T T a U Hr Rj
dZ
dT
C U ÷ + A =
¿
=
µ
Gas-Liquid Agitated Tank- Design Model
Gas-phase Component Mass Balance:


or
(1)


Liquid-phase Volatile-Component Mass Balance:
(2)



Liquid-phase Non-Volatile-Component Mass Balance:
(3)



Energy Balance:


0 ) / ( * * ) )( / ( = ÷ + ÷ Li
o
i
o
L R
i
o
i
i
G
C H P a K E V P P RT Q
0 ) / ( * * ) ( / = ÷ ÷ ÷ Li
o
L R
i
o
i
i
T gas
C H Poi a K E V P P P F
0 * ) / ( * * ) ( = + ÷ + ÷
R inet
Li
o
i
o
L R
Li
o
Li
i
L
V R C H P a K E V C C Q
0 * ) ( = + ÷
R inet
Li
o
Li
i
L
V R C C Q
0 ) ( *
)] * ( * [ )] ( 3 / ) ( 2 / ) ( [
3 3 2 2
= ÷ +
A E ÷ ÷ + ÷ + ÷ E
To Ta A U
R HR V To Ti To Ti To Ti F j
j R i i i
i
i
¸ | o
Three-Phase Gas-Liquid Catalytic Reactor- Design Model
(Trickle-Bed, Fixed-upflow Bubble-Bed, Bubble Slurry Bed,
3-Phase Fluidized Bed)
Non-Volatile Liquid-phase mass balance:



Volatile Liquid-phase mass balance:



Boundary Conditions:

At Z=0

At Z=L

Gas-phase mass balance:



Component mass balance around the catalyst:

0 . 0 ) ( ) ( , ,
,
2
,
2
, = ÷ ÷ ÷ i S i L i c c
i L
L
i L
i L C C a K
dz
dC
U
dz
C d
D
0 . 0 ) ( ) ( ) ( ) ( , , ,
, ,
2
,
2
, = ÷ ÷ ÷ + ÷ i S i L i c c i L
i g
i g L
i L
L
i L
i L C C a K C
Hi
C
a K
dz
dC
U
dz
C d
D
) ( , ,
,
, i L
i
i L L
i L
i L C C U
dz
dC
D ÷ = ÷
0
,
=
dz
dC i L
0 . 0 ) ( ) ( ,
, ,
= ÷ ÷ ÷ i L
i
i g
i g L
i g
g C
H
C
a K
dz
dC
U
0 . 0 ) ( ) ( ,
, ,
= ÷ ÷ ÷ i L
i
i g
i g L
i g
g C
H
C
a K
dz
dC
U
Three-Phase Gas-Liquid Catalytic Reactor- Design
Model (CSTR Slurry)
Non-Volatile Component Liquid-phase mass balance:

(1)


Non-Volatile Component Liquid-phase mass balance:

(2)


Gas-phase mass balance:
(3)



Component mass balance around the catalyst:
(4)


0 . 0 ) ( ) ( ) ( , , , , = ÷ ÷ ÷ i S i L
o
i c c R i L
o
i L
i
L C C a k V C C Q
0 . 0 ) ( ) ( ) ( ) ( ) ( , , ,
,
, , = ÷ ÷ ÷ + ÷ i S i L
o
i c c R i L
o i g
o
i g L R i L
o
i L
i
L C C a k V C
Hi
C
a K V C C Q
0 . 0 ) ) ( ) ( ,
,
( , , = ÷ ÷ ÷ i L
o i G
o
i g L R i G
o
i G
i
G C
Hi
C
a k V C C Q
) ( ) ( ) ( , , i R i S i L
o
i c c R r V C C a K V ÷ = ÷
ReaCat Start up screen
Reaction Reaction Phase Menu
Reactor Type Reactor Type Menu
Inlet Temperature and
Pressure, Energy
Model Selection
Physical Properties
of Components
Reaction Stoichiometry
Rate Law
Reaction Rate Constant
Reactor Specifications
Run
REACTION
Reaction
Phase Menu
REACTOR TYPE
Reactor Type Menu
Global Options
Physical Properties
Reaction Stoichiometry
Reaction Rate
Rate Constant
Reactor Specifications
Feed Composition Input
Heat Transfer Data for Non-isothermal cases
Graphical Output of the ReaCat Program
Reactor Flow-Sheeting
ReaCat, Test Cases
Catalytic Gas Fluidized Bed
Multiple reaction system for the production of Phthalic Anhydride from naphthalene.
“Fluidization Engineering”; Kunii and Levenspiel.(1991, Butterworth- Heinman, P 298)
Literature ReaCat (1) ReaCat (2) ReaCat(2)
Plug Flow Plug Flow Plug Flow Dispersion
Conversion 97% 94.93 % 85.49% 81.26%
(1) – Experimental bubble diameter values has been used by the program
(2) – The correlation of Horio and Nonaka (1984) has been used to find the bubble
diameter.
ReaCat, Test Cases
Continuous Gas-Liquid Stirred Tank Reactor
Liquid phase oxidation of o-xylene into o-methylbenzoic acid
by means of air.
Chemical Reactor Analysis and Design; G.F.Froment and
K.B. Bischoff (1979)
Literature ReaCat
Conversion 83.39% 83.95%
ReaCat, Test Cases
Trickle-Bed
Liquid-phase oxidation of formic acid in the presence of CuO.ZnO
catalyst; Baldi et. Al. 1974, Goto and Smith (1975)
Experimental ReaCat (plug flow) ReaCat (Dispersion)
Conversion 88.5 % 91.0% 89.8 %
ReaCat, Test Cases
Continuous Catalytic Gas-Liquid Slurry Stirred Tank
Reactor
Hydrogenation of Aniline to Cyclohexylamine (Supported Nickel
catalyst)
(Govindrao and Murthy, 1975; Ramachandran and Chaudari 1983 p.
303
Literature ReaCat
Reactor Volume 98 Liter 99 Liter
(46 % conversion of Aniline)
ReaCat, Test Cases
Semi-Batch Catalytic Gas-Liquid Slurry Stirred Tank Reactor
Butynediol Synthesis by the reaction of gaseous acetylene with
aqueous formaldehyde in the presence of copper acetylide catalysts.
; Kale et. Al (1981)
Experimental ReaCat (1) ReaCat (2)
Conversion 62 % 61.0% 68.5 %
1) Adsorption at catalyst surface is taken into account by the program
2) No adsorption effects
Sulfuric Acid Production by Contact Process
SO
2
+ ½ O
2
SO
3
(
(
(
¸
(



¸

÷
|
.
|

\
|
+ + +
=
2 / 1
2 2
3
1
2
3 2
'
2 / 1
2 1
'
2 / 1
2
'
2
'
2
O
P
SO
P
P
K
SO
P
SO
DP
SO
CP
O
BP A
O
P
So
P
SO
r
Where,
P
SO2
, P
O2
,P
SO3
= Interfacial Partial Pressures of SO
2
, O
2
and SO
3
(atm)
P' denotes partial pressures of SO2 and O2 at zero
conversion under total pressure at the point in the
reactor(atm)
K
P
= Thermodynamic Equilibrium Constant, atm
-1/2
Log
10
K
P
= 5129/T – 4.869 T in
o
K
Constants A,B,C,D are functions of temperature.
Parameters and Operating Conditions for the
Sulfuric Acid Contact Process
Inlet Temperature 787
o
F
Inlet Pressure 19.4 Psia
Viscosity 0.09 lb/ft.hr
Reactor Dimensions:
Diameter 2.453 ft
Length 44 ft
Volumetric Flow Rate ( SCFM) 5439.174
Inlet Partial Pressures (Psia):
S0
2
11.08
O
2
7.958
SO
3
0.362
Catalyst Properties:
Density 33.8 lb/ft3
Particle Diameter 0.0405 ft
Bed Voidage 0.45
Graph of Temperature v/s Tube Length for Contact
Process
Graph of Concentration v/s Tube Length for Contact
Process
Graph of Conversion v/s Tube Length for the
Contact Process
SO
2
Conversion v/s Inlet Temperature
0
0.1
0.2
0.3
0.4
0.5
0.6
700 750 800 850 900 950 1000
INLET TEMPERATURE (F)
S
O
2

C
O
N
V
E
R
S
I
O
N
CONVERSION
SO
2
Conversion v/s Inlet Flowrate
0
0.1
0.2
0.3
0.4
0.5
0.6
0.7
3000 3500 4000 4500 5000 5500 6000
INLET FLOWRATE (SCFM)
S
O
2

C
O
N
V
E
R
S
I
O
N
conversion
CONCLUSION

A Package for multi-phase catalytic and non-catalytic
reactors has been developed which demonstrates the
capability to handle complex Material and Energy Balances
and associated correlations.

Features to Be Added:-

+Add a utility to perform reaction rate optimization.
This is very useful when reaction rate is not
known.

+Build a kinetic database of specific industries
such as Sulfuric Acid and Ammonium Phosphate.

Sponsor Documents

Or use your account on DocShare.tips

Hide

Forgot your password?

Or register your new account on DocShare.tips

Hide

Lost your password? Please enter your email address. You will receive a link to create a new password.

Back to log-in

Close