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With Formulas
With Formulas
Simple Sheet
Robert Type Evaporator Design Calculation Sheet
INPUT DATA to be give in
Yellow colour cells
Heating surface
m
2
Inlet vapour temperature
oC
Tube OD
mm
outlet vapour temperature
o
C
Tube thickness
mm
Velocity of inlet vapour
m/sec
Tube Length
mm
velocity of outlet vapour
m/sec
Tube plate thickness
mm
Velocity of condensate
m/sec
Tube expansion allowance
mm
Evaporation rate of the body
Kgs/m
2
/hr
Legment
Author:
Generally Legment taken for Juice heater12mm, evaporators 10mm and for Pan 16mm
mm
Inlet vapour specific volume
M
3
/kg
Tube clearance
mm
outlet vapour specific volume
m
3
/kg
Tube plate hole clearance
mm
proportional factor(
β)
Author:
Generally β value take for multiple pass 0.6 to 0.8 and for single pass 0.8 to 1.0
Percentage of downtake Dia on tube plate area of tubes
Author:
According to peiter rein down take dia consider less than 25% of the tube plate dia (p.no. 297)
According to Hugot The diameter of the centre well varies from ¼ to ⅛ of the interior diameter of the vessel. ( pg. no. 509)
%
S.No
Description
UOM
Value
Formula
1
Number of tubes
Mean dia of the tube ( Dm)
mtr
Tube OD- Tube Thickness
Effective Length of the tube ( L )
m
Tube lg - 2(Tube plate thk)-2(Tube expansion allowance)
No. of tubes
no.s
Heating Surface =
π
D L N
2
Tube plate & Downtake dia
a
Area occupied for tube plate
Tube Pitch (P )
mtr
OD+legment+tube clearance+hole clearance
Taken extra dia for stay roads arrangement or multiple down take arrangement
%
Tube plate area required for tubes only
m
2
(0.866 x P
2
x N /β)
x %extra
Tube plate Dia required for tubes only
mtrs
SQRT ( A x 4/
π
)
mm
b
Dia of the single down take
Dia of the down take
mm
Tube plate dia for tubes x % of downtake on tube plate
Area of the downtake
m
2
π
r
2
Total area of the tube plate
m
2
Area of the Tube plate for tubes + Downtake area
c
Final Dia of the tube plate
mtr
SQRT ( A x 4/
π
)
mm
d
Dia of the
multiple down takes
Consider each peripheral down take dia
mm
Consider number of peripheral down takes
no.s
Total area of peripheral down takes
mm
2
π
r
2
x
number of peripheral down takes (r = radious of each peripheral down take
Available area for central down take
mm
2
Area of the single downtake - Total area of peripheral down takes
Dia of the central down take
mm
SQRT ( A x 4/
π
)
3
Dia required for vapour inlet
and Dia of the Calendria in radial steam/ vapour entry
Number of steam/ vapour entries
no.s
Author:
If the sibgle entry than take value = 1
Evaporation rate of the body
Kgs/m
2
/hr
Vapour required for calendria
Kgs/hr
Heating surface x Evap. Rate
m
3
/sec
Multiptiplyed by specific volume of vapour
Total area for vapour entry ( A )
m
2
A = Q/ V
a
Dia of the each steam entry
mm
SQRT [ (A / Number of steam/ vapour entries)
x (4/
π
) ]
Say
mm
b
Calendria dia at the entry of the steam/vapour jocket
Area of each steam entry
mm
2
π
r
2
Height of the steam entry
mm
Take Effective Length of the tube
Width of the steam entry
mm
A = L x W
c
Dia of calendria at the point of radial steam entry
mm
It is to be maintained at the vapour entry side
later it may reduced in vapour travel direction.
4
Vapour outlet pipe dia
Vapour volume
m
3
/sec
Heating surface X Evap. Rate x Specific volume of vapour/3600
Vapour outlet pipe dia
mtr
SQRT [vapour vol./(0.785 x velocity of vapour)]
Say
mm
5
Dia of the condensate line
Volume of the condensate
kgs/hr
Heating surface X Evap. Rate
m
3
/sec
Here considered density of water as 1 and also consider 10% extra for free removal of condensate
No. of condensate withdrawals
no.s
Condensate pipe dia each
mtr
SQRT (vapour vol./(0.785 x velocity of condensate))
mm
6
Noxious gases
Cross section area of non condensable gases
cm
2
No. of NCG withdrawal points
Dia of the each non condensable gases line
cm
SQRT( 4*area./3.14*no. of points)
Say
mm
7
Vapour space height
Take
Author:
Generally for Robert type bodies taken for lost effect 2.5 times on calendria tube height and for remaining bodies take 2 tmes on Calendria tube height
Generally for Robert type bodies taken for lost effect 2.5 times on calendria tube height
and for remaining bodies take 2 tmes on Calendria tube height
mm
8
Velocity in vapour space of body (Cross checking of the system )
Vapour volume
m
3
/sec
Heating surface X Evap. Rate
Crossectional area of the body
m
2
Velocity in vapour space of body
m/sec
Author:
vapour velocities in the vessels maximum reach 3.6m/sec and for lost body reach maximum 4.6 m/sec . And If more than 6m/sec than entrainment chance is more.
The velocity of vapour leaving the liquid surface would then be approximately 10 cm/sec
Ft/sec
9
Calendria shell thickness
(
P*
Di / (2*F*J - P)
) +
C
P = Maximum allowable pressure
kg/cm
2
Di = ID of the Calendria
mm
F = Allowable stress
kg/cm
2
J = Joint efficiency
C= corrosion allowance
mm
Calendria shell thickness
mm
Say
mm
10
Vapour shell thickness
(
P*
Di / (2*F*J - P)
) +
C
P = Maximum allowable pressure
kg/cm
2
F = Allowable stress
kg/cm
2
J = Joint efficiency
C= corrosion allowance
mm
Di = ID of the Calendria
mm
OD - 2 x Calendria shell thickness
Vapour shell thickness
mm
Say
mm
11
Tube plate thickness
C= corrosion allowance
mm
F = Allowable stress
kg/cm
2
P = Maximum allowable pressure
kg/cm
2
E
s
= Modulus factor for MS sheet
kg/cm
2
E
t
= Modulus factor for SS sheet
kg/cm
2
G = ID of the shell
mm
OD - 2 x Calendria shell thickness
t
ts
= Thickness of the shell
mm
t
t
= Thickness of tube
mm
d
o
= OD of the tube
mm
D
o
= OD of the calendria sheet
mm
N
t
= Number of tubes
no.s
K
K =
(
E
s
x t
s
x (D
o
-t
s
)
)
/
(
N
t
x E
t
x t
t
x(d
o
-t
t
)
)
f = safety factor
f = SQRT
(
K / (2 + 3K)
)
Tube plate thickness
mm
f x G x SQRT
(
(0.25 x P)/F
)
+ C
12
Vapour doom dia
On vapour o
utlet line area
Author:
Generally for Robert type bodies vapour doom dia taken 2 to 2.5 times for vapour outlet pipe area
Generally for Robert type bodies vapour doom dia taken 2 to 2.5 times for vapour outlet pipe area
Cross sectional area of the vapour doom
mm
2
Vapour doom dia
Say
mm
Top cone angle (
φ)
Deg
Top cone height
Tan
φ
(
(ID of body
-ID of doom)/2
)
13
Center Umbrella area
a
Case 1 (cross sectional Area
of the body - cross sectional area of the doom = area of Umbrella
mm
Author:
In some designs consider 60 to 65% on body dia
Case 2 (While considering 65% on body dia)
mm
Here Case 2 considered
Gap between Umbrella to top cone at entry H
mm
π * Dia of Umbrella* H = Area of vapour doom
Gap between Umbrella to top cone at exist H
mm
"0"
π * ID of doom* H = Area of vapour doom
Robert Type Evaporator Design Calculation Sheet
INPUT DATA to be give in
Yellow colour cells
Heating surface
m
2
Inlet vapour temperature
o
C
Tube OD
mm
outlet vapour temperature
o
C
Tube thickness
mm
Velocity of inlet vapour
m/sec
Tube Length
mm
velocity of outlet vapour
m/sec
Tube plate thickness
mm
Velocity of condensate
m/sec
Tube expansion allowance
mm
Evaporation rate of the body
Kgs/m
2
/hr
Legment
Author:
Generally Legment taken for Juice heater12mm, evaporators 10mm and for Pan 16mm
mm
Inlet vapour specific volume
M
3
/kg
Tube clearance
mm
outlet vapour specific volume
m
3
/kg
Tube plate hole clearance
mm
proportional factor(
β)
Author:
Generally β value take for multiple pass 0.6 to 0.8 and for single pass 0.8 to 1.0
Percentage of downtake Dia on tube plate area of tubes
Author:
According to peiter rein down take dia consider less than 25% of the tube plate dia (p.no. 297)
According to Hugot The diameter of the centre well varies from ¼ to ⅛ of the interior diameter of the vessel. ( pg. no. 509)
%
S.No
Description
UOM
Value
1
Number of tubes
2
Tube plate & Downtake dia
a
Area occupied for tube plate
Taken extra dia for stay roads arrangement or multiple down take arrangement
%
Tube plate Dia required for tubes only
mm
b
Dia of the single down take
mm
Final Dia of the tube plate
mm
d
Dia of the
multiple down takes
Consider each peripheral down take dia
mm
Consider number of peripheral down takes
no.s
Dia of the central down take
mm
3
Dia required for vapour inlet
and Dia of the Calendria in radial steam/ vapour entry
Number of steam/ vapour entries
no.s
Author:
If the sibgle entry than take value = 1
a
Dia of the each steam entry
mm
Say
mm
b
Calendria dia at the entry of the steam/vapour jocket
Dia of calendria at the point of radial steam entry
mm
4
Vapour outlet pipe dia
Vapour outlet pipe dia
mtr
Say
mm
5
Dia of the condensate line
No. of condensate withdrawals
no.s
Condensate pipe dia each
mtr
mm
6
Noxious gases
No. of NCG withdrawal points
Dia of the each non condensable gases line
cm
Say
7
Vapour space height
Take
Author:
Generally for Robert type bodies taken for lost effect 2.5 times on calendria tube height and for remaining bodies take 2 tmes on Calendria tube height
mm
8
Velocity in vapour space of body (Cross checking of the system )
Velocity in vapour space of body
m/sec
Author:
vapour velocities in the vessels maximum reach 3.6m/sec and for lost body reach maximum 4.6 m/sec . And If more than 6m/sec than entrainment chance is more.
Ft/sec
9
Calendria shell thickness
P = Maximum allowable pressure
kg/cm
2
F = Allowable stress
kg/cm
2
J = Joint efficiency
C= corrosion allowance
mm
Calendria shell thickness
mm
Say
mm
10
Vapour shell thickness
P = Maximum allowable pressure
kg/cm
2
F = Allowable stress
kg/cm
2
J = Joint efficiency
C= corrosion allowance
mm
Vapour shell thickness
mm
Say
mm
11
Tube plate thickness
C= corrosion allowance
mm
F = Allowable stress
kg/cm
2
P = Maximum allowable pressure
kg/cm
2
E
s
= Modulus factor for MS sheet
kg/cm
2
E
t
= Modulus factor for SS sheet
kg/cm
2
Tube plate thickness
mm
12
Vapour doom dia
On vapour o
utlet line area
Author:
Generally for Robert type bodies vapour doom dia taken 2 to 2.5 times for vapour outlet pipe area
Vapour doom dia
Say
mm
Top cone angle (
φ)
Deg
Top cone height
13
Center Umbrella area
a
Case 1 (cross sectional Area
of the body - cross sectional area of the doom = area of Umbrella
mm
Author:
In some designs consider 60 to 65% on body dia
Case 2 (While considering 65% on body dia)
mm
Gap between Umbrella to top cone at entry H
mm
Gap between Umbrella to top cone at exist H
mm
"0"
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