Total Process Engineering Manual
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“S
t
TOTAL
bbb
2ROCES.S
ENGINEERING
INDEX
TEP/DP/EXP/SUR
.
c
J
1.
DSIGN
2*
VEJjSEL!5
J
3.
StlhlKq.
(vapour-liquid
separators)
.
.
Tray Packed
* . HEAT
4-
. .
EXCHANGERS .
Plare exchangers Furnaces
.
Steam
. .
P through valves and fittings Conrrol valves - sizing and selection
.
Gas sweerening
. .
Air Drainage
.
Shell + tube Air coolers
PUMPS
5. ‘II,
S6UM
/
.
Cenrrif ugal Reciprocating l
DRIVERS
6.
v/
Gas turbines Electric drivers
/
7,
COMPREssoRs
/
8.
EXPANDERS
9-,
FLARE
10.
PIPES
J
J I ‘c
.
11. I
J
.
4
Line sizing Piping classes
Pressure
PACKAGE
and temperafure
drops
UNITS
Dehydrarion Ref rigeratlon
:
/4 . 13.
+ FlTTINCS
PIPELINES *
12.
Turbines
SYSTEMS VALVES
UTILITIES
-
Water tiitrogen
14,
COMPUTER.
PROGRAMS
15.
DATA
16.
PROC E5S CALCULATION
17.
PROCESS
DATA
SHEETS
StiEETk
o
: 2,85
COLUMNS
J
/
NlAliHhrJl~=
Date
CONDITIONS
Horizonral Verrical
.
Revision :
MANUAL
DESIGN
Page No :
0
-
.
.
TOTAL
I PROCESS
ENGINEERING
DESIGN
/ TEPIDPIEXPISUR
MANUAL
Revision
:
Date
: 2J85
Page No :
i
.
1.
DESIGN
CONDITIONS
TOTAL
PROCESS
ENGINEERING DFICN
TEP/DP/EXP/SUR
DESIGN
MANUAL
CONDITIONS
Revision
: 0
Page No :
Date
:2/8S
L-1
1. APPLICABILITY The
fol owing
design
criteria
are
applicable
for
both
feasibility
studies
and
pre-project
studies.
.
The design Operating o-
pressure
of a vessel
pressure barg
Design
10
IO-
50
so - 100 > 100 Vessels
.
subject
to vacuum
pressure
If the Internal
.
- 1 bar
MOP
+ 10 %
MOP
+ 5 barg
during
pressure
for
pump
pumpA
P when operating
as of rhe following - Note
-: Pnin
= 3.2
i
SaraI
?rocess
.* i
Operating
Pressure I
+ 5 36 shall
be designed
for
the maximum
external
I
of 0.15 bar. or less the vessel
discharges at design
shall
will
be calculated
be designed by taking
for full
I
vacuum.
120 % of the normal I
conditions.
I:
TEMPERATURES
Design
vessel
temperatures
shall
be as follows
:
I
Maximum
design
temperature
=
max.
operating
Temp
+ 15 “C
iMinimum
design
temperature
=
min.
operating
Temp
- 5 “C
or minimum .
;
1MOP = *Maximum
operation
is 0.35 bara
Design
3.0 DFClIGN
MOP
plus a margin
pressure
be taken
pressure barg
* MOP
operating
.
shall
Consideration depressurisation (See section
for
the
minimum
of the vessel
design
that
may
ambient temperature
occur
during
temperature. must emergency
take
into
account
or shut down
any
situations.
on flaring). .
4,OMATERIALOFCONSTRUCTION .
Details Taole
.
Details
of the required
material
of construction
for
various
temperatures
are given
1. on corrosion
allowances
and wall thickness
are given
in the vessel design
section.
In
TOTAL
I
PROCESS
ENGINEERINb DESIGN
LJC~IUIU
JVIMIWUM~
,,o.*a.v..
.
Date
: 2435
CONDITIONS
TEP/DP/EXP/SUR
.
.- .
____-------
-‘I’ $ I ; _L
h u I
: c
“-G” hg:“- 3 cz-uu” __---------
. : . *-m . ;
: . --. I
..-L&,,,--I------
--A-----
_-----em
---
-----
--------
: ,7 8
.------
.
--------L-m n % 2 :i
_---w----e
-
1.2
I
-! I
rOTAL
PROCESS ENGINEERING
DESIGN MANUAL
I-EP/DP/EXP/SUR
.
f
. i 4 I 1I I
2,
VESSELS
1
Revision
:
Date
: 2/85
PageNo:
TOTAL
PROCESS
VAPOUR
TEP/DP/EXP/SUR
DESIGN
ENGINEERING
- LIQUID
MANUAL
Revision
: 0
Page NO : TEP
SEPARATORS
Date
WI5
2.1 3.
APPLICABILITY Virtually
all process
of a separator
schemes
with
use phase separation
acceptable
accuracy
of some
description.
for
the
is required
both
The design
feasibility
and.sizing
and
pre-project
phases. Consideration separators
for
concerning
vessel
Separation
of solids
vendor
will
from
for details
SEPARATORS
Provide
tripping
System
are
also
given
is not
covered
in this
designed
design
guide.
Generally
a
vessel.
w I
vertical
unless
I
stated)
Gas KO drums of
liquid
from
sufficient
KO drum
upstream
Always
vapour
surge
time
- See section
of
acid
required.
Always
(1 to 2 minutes)
9.0 Flare
gas absorbers,
Can be incorporated
use demister
into
consider
between
a mist
the HLL
and
Systems
glycol
confactors
base of tower
bd
and dessicant
for weight
b-
and space saving.
I
pads. 4.
Production
separators
(Vert
or horizontal)
L lquld
separation from gas not compressor is located immediately start-up, 3 PHASE .
Details
horizontal
Feed KO drums
dehydrators.
2-2.
and
the compressor.
Required
.
vertical
CONSIDERATIONS
(usualy
and Fuel
eliminator.
Unit
of
separation.
of a proprietory
AND
separation
.
specification
vapour-liquid-liquid
gas or liquids
Efficient
Relief
the
to
internals.
Comoressor
.
section
and
APPLICATIONS
2 PHASE .
this
vapour-liquid
be consulted
SWARATOR 2.1.
in
is given
shut-down
and process
as critical
as compressor
downstream
slugs when
of
KO
separator.
drum Always
unless
a
consider
designing.
SEPARATORS
3 phase
production
separators
entrainment
is required
water
must
Chemical
phase
additives
are
demisters
be sufficient (demulsifiers,
horizontal.
generally are
usually
SO as not
anti-foam,
stated.
to overload pour
point
If good Oil
liquid-vapour
separation
water depressants)
from
de
I
the
treatment
units.
may
be added
I
to aid separation. I
jMc--
PROCESS
ENGINEERING
DESIGN
Revision
MANUAL
:
0
-
VAPOUR
- LIQUID SEPARATORS
I Date
TEP/DP/EW/SUR
: Y85
I
I -’
‘- 3. HORIZONTAL 0
OR VERTICAL
Provided
I
sufficient
vertical I
i
L/D ratio is selected a horizontal
.
Vapour velocity in a horizontal drum can exceed the liquid L/D > 1. For vertical drums the velocity cannot.
.
Horizontal
is more efficient
than a
drums are more effective than venical
and geometrically
settiing
more
velocity
practical
provided
for a heavy
drums.
.
drum does not alter the vapour flow area. A rising liquid level in a vertical Consequently vertical drums are preferred for compressor and fuel gas KO drums.
.
Vertical drums utilise a smaller plot area and are easier to instrument with alarms and shutdown controls. For floating installations are preferred as less “sloshing” occurs.
.
For high volume flowrates a split flow horizontal drum is preferable as smaller drum diameters can be used. The preferred split flow arrangement is a single centre entry nozzle with two end exists. Head exits can be used where plot space is limited.
.
Each design case must be evaluated as a guideline :
I
c
separator
for the same flow area.
liquid phase removal
I
DESIGN
-
Vertical
-
Horizontal
.
drums
drums
separately
but in general
Compressor KO drums Fuel gas KO drums Floating installations Production separators 3-phase separation
the following
can be used
Degassing boots Absorber feed KO drums
HP
Try to avoid vessels with wall thickness greater fabrication and can prove expensive.
Ref lux drums Flare KO drums than 100 mm as these require
4. CALCULATION THEORY AND EQUATIONS (for use in calculation sheets) (Valid only for pure gravity settlers with no internals to enhance separation) 4.1.
LIQUID-VAPOUR 0
02.
Vs = K
K =
[F]”
SETTLING
VELOCITY P;;: 1 :Jzi;;z;r;lity
K = correlating parameter m/s D - panicle diameter -microns C - drag coefficient c,-
03.
Vs =
kg/m3
vapour viscosity
- centipoise
special
PROCESS
TOTAL
ENGINEERING
VAPOUR
TEP/DP/EXP/SUR
- LIQUID
DESIGN
MANUAL
SEPARATORS
Revision
Date
: 0
Page No :
f TEP/DP ..J
2.3
a/s5
(see p: .
For medium and low pressure- with gases can be used to estimate Vs.
.
For higher pressures (> 50 bar) or viscosities in excess of 0.01 cp it is necessary to calculate Vs. The drag coefficient C is calculated using Figure 2 (curve 2) where :
Equation 4.2.
3 is then used to calculate
LIQUID-LIQUID (based on Stokes
of
viscosity
less
than
0.01
cp
Figure
1
Vs.
SETTLING VELOCITY law of terminal settling)
The following equation can be used for calculating the settling velocity of water in oil or the upward ‘!settling” of oil in water. The important fact is to use the viscosity of the continuous phase i.e : for oil settling upwards through water use the water viscosity, for water settling in oil use the oil viscosity.
ut =
terminal velocity = gravitation accel fi = density heavy fluid P L = density light fluid c= viscosity (continuous)
P
Setting the particle
05. .
.
m/s m/s2 kg/m3
4
kg/m3
kg/m-s
size to I25 microns and using more useful units gives :
\I
Ut = 0.513 (p,;--
)
‘~~~~~ntipoise
The above equation is valid for REYNOLDS no of 0.1 - 0.3 If calculated settling velocity is > 250 mm/min use 250 max
I
I
I 4.3.
VESSEL VOLUMES .
Partial volumes of a horizontal cylinder can be calculated using rhe partial volume charts in Figure 3 or estimated using the following equations : (for vessels with a diameter < 1.2 m ignore head volumes)
I I I
PROCESS ENGlNEERlNG .
- LIQUID
VAPOUR
Revision
:
Date
?/85
DESIGN MANUAL
0
Page NO :
SEPARATORS
; TEP/DP/EXP/SL’R ..
*
AL - D2 D - 2h 4 Cos-1 ,~,-@-~,-hi’,2
(see page 2.13 for sketch)
2”
1
t HORIZONTAL 2 DISHED
0
HEAD
2 ELLIPTICAL
HEADS
2 HEMISPHERICAL
These
formula
More
Vhh = 1.047 h2 (1.5 D - h)
m3 (most m3 (gives
common) extra
vol)
For
accuracy
h:
(1.5D-h)
+ AL-B
for general
design
and are easily
programmed
saving.
are available,
see ref list,
but are often
too complicated
calculations. the
between
length
L should
nozzles.
This
be the
tan-tan
is especially
true
with
length
and
large
vessels
not
the and a
design.
CALCULATION A guide
formula
length
enough
for time
for multiple
greater
tight
0.52194
2
are accurate
accurate
flowpath
4.4.
h2 (1.5 D - h)
heads)
to be useful .
Vel = 0.52194
=
on to a calculator
Y r
h2 (1.5 D - h) m3
h
(elliptical
.
in radians
Vdh = 0.21543
HEADS
for depth
n
m3
VOLUMEUPTOBAFFLE
. .
.
Vc = AL.L
CYLINDER
PROCEDURE
for filling
.
Decide
.
If applicable a mist
VERTICAL
in the attached
if Figure
calculation
1 can be applied
recommended
will to install
Vs using
equ 3.
Derate
the
curve
be installed) a mist
(vapour-liquid
separation)
sheet.
i.e P < 50 bara,,u
use the 500 micron
eliminator
VESSEL
to evaluate
settling
or 150 micron
eliminator
for
< 0.01 cp
with
most
velocity no mist
(this assumes eliminator.
applications.
It is
If not calculate
I .
maximum .
1 ’
allowable
Calculate
drum
adjustment .
Check
calculated
settling vapour
internal
by
85
% design
margin
to
give
a
velocity. diameter
of ID : OD can be made
if wall thickness
velocity
is less than
and
round
to nearest
to suit standard 100 mm
(See 4.8).
50 mm.
(note
further
head dimensions).
I
TOTAL
PROCESS
ENGINEERING.
VAF’OUR
TEP/DP/EXP/SUR
- LIQUID
DESIGN
MANUAL
Revision
:
0
Date
: 2fsr
Page No :
SEPARATORS 2.5 1i
I
calculate
.
:
I.
hl - max (15 8 of b or 400 mm)
I
h2 - 100 mm if mesh selected 150 mm for Compressor KO
I
vessel height based on following
criteria
hl
I
h3 - max (50 % of !J or 600 mm)
h2
4
‘*F
If no mesh use hl + h2 + h3 = 60 % 0 or 800 mm
I
h4 - 400 mm + d/2 : d = inlet nozzle @
I
h5 - calculate based on l-2 minutes residence time at maximum liquid inflow - min 200 mm
I
h3
h4
h6
h7
I
Lu
h8 l?.
-c, L
h6 - base on following hold up times : (min 350) 4 min - reflux drums with pump 5 min - product drums no pump 3 min 8 min - heater feed 4 min. - HP sep. to LP sep.
I
1
I
I !
h7 - 1-2 min residence time - minimum h8 - 150 mm for bottom connected LC 300 mm for side connected LC
150 mm I I
I I Note
:
For compressor suction drums that are normally dry set HLL at 450 mm above tan line and use bottom connected LC. This will reduce vessel I I * height if required. No specific HLL-LLL hold up time required:
I I .
I I
1*
r
-, TOTAL
PROCESS
DESIGN MANUAL
ENGINEERJNG
VAPOUR - LIQUID
CALCULATION
PROCEDURE
HORIZONTAL
A guide on how to fill in the attached 1. Calculate 2. Derate
calculation
this by F = 0.85 and calculate
Vm = F x Vs x (L/D) m/s
size 350,
,
vapour velocity
V m/s
use L/D of 3 to 4 max (3 initial
esr)
area, Av
liquid surge volume, calculate
L (note if L/D changes significantly
2.6
, use Fig. I or equ. 3.
4. Assume drum is 70 % full i.e h/D = :7 and evaluate (to nearest 50 mm). For “drq’ vessels de h/D = .35
drum 0 to give required
vol at HLL, if insufficient
adjust
Av
D or
recheck Av using new Vm).
6. Set position of LLL in drum and confirm volume is insufficient
.a83
sheet.
required
required vapour cross sectional
5. For required
Date
Page No :
0
VESSEL (Vapour-liquid)
settling velocity Vs for par&al
3. Evaluate
:
SEPARATORS
TEP/~P/EXP/SUR
4.5.
Revision
required
increase 0, L or h. Include
surge
vol between HLL-LLL.
If
volumes in heads.
7. When setting LLL height take into account any LSLL, LSL alarms and vortex breakers which may set minimum value usable. Usually 300-350 mm. 8. Rationalise
all heights and dimensions to nearest 10 mm.
NOTES : .
For high volumetric flows of gas with small liquid volumes consider using split flow arrangement. Design is as above but with half vapour volume flow.
.
Normal (primarily
design is with top entry, offshore)
exit nozzles.
However
if space is limiting
head mounted nozzles can be used to increase flowpath.
.
L is designated as the flow path length i.e distance between inlet and outlet nozzle. 1’ is the tangent-tangent lengh. For 1st estimates 1’ = L + 1.5 pi + 1.5 D2 pi = inlet nozzle diameter 02 = outlet nozzle diameter
.
“Normal”
liquid levels are taken as midway between the high and low levels.
rOTAL
PROCESS ENGINEERING VAPOUR
TEPIDPIEXPISUR
4-6,
CALCULATION .
- LIQUID
PROCLDURE
DESlGN MANUAL
Revision
:
Date
: 2/85
with
estimate)
TEP/f
HORIZONTAL
2. Provision
3. Calculate Inspection
mixture
Use L/D
as well
as
! 1
= 3 (lst j
L.
now has to be made
Use Tan-Tan
2-7
VESSEL 3 PHASE (See Figure 4)
steps 1 to 4 as for a two phase separation.
and evaluate
Page NO :
SEPARATORS
Sufficient residence time to allow separation of the oil-water the oil surge and vapour flow areas must be provided.
1. Proceed
0
TC
to
accomodate
bath oil and water surge volumes.
I
length L’ and not nozz-nozz distance L. LLL required to give approx 4 mins oil surge capacity (minimum). I will reveal whether sufficient height exists below LLL to include the
interface
levels. If not, adjust the vessel bar L to give sufficient
room.
Note :
If the water cut is very small, consideration may be given to using a water boot instead of a baffle arrangement see step 10. I
/
4. Having determined HLL and LLL now set both position and height of baffle. Calculate terminal settling velocity of water droplet (equ 5 sect 4.2) at both HLL I and LLL. Volumetric flow of liquid is in both cases the oil plus the water. Calculate fall distance of a droplet across length of the drum. Baffle height and I position can now be set noting : -
the baffle the baffle
should be at least 75 mm below the LLL should be at least 2/3 down the length of the drum from the inlet in some cases the water droplets will settle to the floor in a short distance. The baffle should still be set at a minimum of 2/3 along the vessel.
5. Set the HI1 at baffle height - 75 mm. The LIL according vortex breaker + LSLL use a minimum of 300-350 mm.
to height determined
1
I
t i *Ip
ab
6. Check if an oil droplet will rise through the water layer (from drum floor) to LIL before reaching water outlet. Use area at LIL with normal oil + water flowrates. (This criteria is very rarely governing but must be checked). 7. Calculate water surge time XJ.8 outlet. Remember to baffle. LMtnimum acceptable consider using a water boot
/
.*
I Vol HIL - Voig LIL, and residence time Vol NIL use only one head volume, and length of drum upto times are 4-5 mins. If calculated times are very long I arrangement.
8. Rationalise all dimensions and “tidy” levels to standard values if possible i.e : I 150 mm, 200, 250, 300 etc. This allows use of standard displacers. 9.
Recalculate Note
:
all residence
times
based on “tidied”
levels
(if required).
In calculating
the final residence times make sure that the vessel tantan length is used and not the nozzle to nozzle distance L.
-
-
I
dTOTAL
PROCESS
* i1 TEP/DP/EW/SUR
/
VAPOUR - LIQUID
10. Boot calculation. 1s
ENGlNEERlNG
DESlGN
MANUAL
Rwision
:
Date
S/85
SEPARATORS
0
Page NO :
2.8
(See Fig. 5)
If the water volumetric flow is so small as to not warrant a separate baffled . settling compartement as detailed above a water boot should be used instead. To design proceed as follows :
I
Sf !
5.
I
).
I
1. Proceed as previous upto step 3. 2. Calculate settling distance of water droplet when vessel is operating at LLL. Water droplet should reach floor of drum before oil outlet. Remember that the oil exit nozzle will be raised above the floor as a standpipe. Adjust drum 0 or L to achieve settling.
le
3. Check that settling is also possible when operating below drawoff nozzle level.
II
at HLL,
droplet
to fall
a 4. Size water drawoff boot 0 (try to use standard pipe diameters). Calculate rising velocity of the oil in water, set downward velocity of water in boot at 90 ,% of this and evaluate boot 0. Boot length by inspection (use standard displacers).
I .e. 4 -.
Note
d
I
:
Boot 0 must be less than 35 % of vessel 0 When heavy walled vessels are used a remote boot may be more economical to prevent large cuts in the main vessel.
I
4.7.
NOZZLE
SIZING (see section 10.0 also)
:.
Inlet nozzle
I
. . .
di
Size based on normal volumetric
flow + 10 % (liquid + vapour flow
Limit inlet velocity to 7 - 13 m/s Round nozzle diameter up or down to nearest standard
size
L i.
Gas outlet . Size on normal flow . Velocity limit 15-30 m/s
I
_I 0
.
Manholes : 450 mm or 60G
Liquid outlet . Normal flow + 10 % . Velocity limit l-3 m/s HC 2-4 m/s water . Min. diameter = 2” (avoid plugging)
g I 4.8. : I
I
-I
VESSEL WALL THICKNESS Calculate vessel wail thickness thickness should be calculated t < 100 mm.
using the ASME VIII div. I formula. The wall immediatiy after D is known to confirm if
QTAL
PROCESS
ENGINEERING
DESIGN
VAPOUR - LIQUID
TEP/DP/EXP/SUR
MANUAL
SEPARATORS
I
t
=
PD ZSE - 1.2P
C = corrosion
Revision
: 0
Date
*Z/85
I
-D t P
+c
allowance
mm
- use 3 mm unless stated otherwise by EXP/TRT
Page No :
2.9 I
I
= Z
diameter mm wall thickness mm = design pressure barg E = joint efficiency use 1 for seamless shells .85 otherwise s = max. allowable stress bar use 1220 bar for CS plate 1000 bar for SS plate for t < 100 mm : no fabrication problems 100 < t < 150 mm : vendor advice may be needed t > 150 mm : Major fabrication problems
In order to meet standard vessel head sizes and wall thicknesses the following ranges should be observed : Vessel diameter : 250 - 1250 mm in increments of 50 mm i.e. 250, 300, 350... 1300 - 4000 mm in increments of 100 mm i.e. 1300, 1400, 1500... Standard wall
:
of 1 mm
30 - 60 mm in increments of 2 mm 60 - 140 mm in increments of 5 mm
thicknesses
4.9.
1 - 30 mm in increments
5--1
i.e. 1, 2, 3, B... i.e. 30, 32, 34, 36... i.e. 65, 70, 75, 80...
5.:
VESSEL WEIGHT weights either horizontal or vertical can be estimated using Fig. 5. This figure j I is for the steel shell including manholes, nozzles, fittings etc but not the removable / I internals or support skid. The heads can be estimated by using weight of 2 heads = ,, (m) x wall thickness (mm) x 20 kg.
Vessel
5. VESSEL INTERN& 5.1.
MIST ELI,MINATORS 6.0 .
.
R
tMist eliminators or mesh pads are located under the vapour outlet nozzles of aI1 compressor suction drums and fuel gas KO drums. For production separators it is always gaod practice to install an exist mesh pad.
6
For dirty or and high viscosity vendor for futher data. .
6
liquids the efficiency
falls to approx. 75 %. Consult
6
‘TOTAL
PROCESS ENGlNEERlNG
Revision :
DESIGN MANUAL
VAPOUR - LIQUID SEPARATORS
.L
?I=
Date
TEPIDP/EXP/SUR
0
Mesh is usually made from 304.55. YORK DATA as follows
.
York no
Types of pad : General purpose High efficiency
431 421 326 931 644
Dirty service
.
)e 5.2.
kg/m3
Thickness mm
144 192 115 80
The engineer should specify type, diameter the vessel data sheet.
.
:
Residual* ’ entrainment
100 100 100 150 150
5.3.
and thickness
of pad required
For particle sizes of 5 microns or less use two pads spaced 300 mm apart eg : . giycol contactor.
LIQUID
.
i IIP -)r
.
c
.
all is
on
INLET INTERNALS
I re
PPM
1.0 - 1.2 -55 - .61 -17 - 0.19 1.6 - 1.8 .8 - .87
Inlet internals can be specified to aid feed distribution and promote separation. Generally for pre-project stage details are not required.
I/
2-10
A
-
I
Page NO :
vapour-liquid
PHASE INTERNALS
Vortex breakers should be detailed for each oil/condensate outlet where the oulet flow direction is vertical. Vendors will sometimes specify internal packs of tilted arrangements to promote phase separation.
and produced water
plates or baffles or other
Sand jetting facilities should be provided for on services where there is a risk of silting or sediment build up in the vessel. Generally jetting facilities are not required on gas-condensate systems.
6.0 REFERENCES
AND USEFUL LITERATURE
6.1.
LUDWIG VOL I CHAPTER
6-2.
PERRY CHAPTER
6
6.3.
Program calculates
partial
4
I ult
I I
volumes Pierre Koch OGJ Dec. 3 1983
i
Operating
data
Pressure
:
(operating)
Temperature
(operating)
bata
=
l-04-
“C
=
34
=
51-b
Liquid
description
kgfhr
=
7
Liquid
flow
kg/m3
=
2-i
Liquid
density
m3/s
=
1
Actual
volume
Particle
size
Gas ,MW Gas flow
rate
Wg
Gas density Acrual
T, P
volume
,Mesh pad
flow
Qg
.Ye J No
1. Vawur-liquid
3
‘?.qO
rate
=
(T,P)
kg/m3
=
flow
m3/min
=
2.23
microns
=
Iso-
.
Estimate
:
.
If P < 50 bar and
/^
< 0.01
use Fig.
.
If P > 50 bar or
,+
> 0.01
use calculation
settling
velocitv
: from
or calculated
Fig
Figure
1 and 500 micron
1
4co
BIO
rs
h6
h’ II h8
1 and 150 microns
it
for Vs
I-6
7.
m/s
vs =
;
1~4
line
vs =
C =
0.L
kg/hr
:
Vs using
CQ3E
:
-w
.
m/s
, 2.
Derating
3.
Actual
maximum
% = 85
Drum
volumetric I
=
gas flow
velocity
flow
a+5+3
5.
Required
liquid
hold-up
times,
l
\-36
area
=
m/s
0-s
m2
Calculated drum D = too0 arCn ..Yk bpCCII.A~ 5 2 uapu
m3/s
SELECTED
4..
Vm 5
DIAMETER -64
L\9..3
=
mm
* II*
mm
2500 -
ha * = c.q&
a3CrA.d
HIA- --LLL
;.
8.
V
h5 :
HLA
- HLL
=
2.
min
=
i-b
m3
=
400
mm height
t
h6 :
HLL
- LLL
=
5
min
=
It*15
m3
=
z-r50
mm
L
h7 :
LLL
- LLA
=
2.
min
=
4-4
m3
=
900
mm
D
,Mesh pad :
Q
e /no
thickness
=
too
mm
Sheet PROCESS,
m-4-7
CALCULATION
TOTAL TEfKxF/MP BY
/ EXP/ SUA CHK
OATE
VAL’OUR-LIQUID JOB -___-~
TITLE
SEPARATOR EXAr?td
.-I
S&ET ITEM
VERTICAL
1 of 2
NO JOB
:
:
DEqAss’~4
D Ho
r50aT
123+
E.XhHtLf
REV
m
‘(\ f .
r 1. 5eight ?
=
. 0
calculation
2500
mm
hl :
I5 % of 0 or 400 mm (Use max)
mm
h2 :
mesh pad 50 % of P or 600 mm
mm
mm
h3 : . With mesh : hl + h2 + h3 No mesh : hl + h2 + h3 : 60 % 0 or 800 h4 : 400 mm + d/2 : d = inlet notz 6 h5 : From step 4 or 200 mm h6 : From step 4 or 350 mm h7 : From step 4 or 150 mm
For “dry”
Wall
550
mm
900
mm
2250
=
DESIGN
.
CORROSION
so0
mm
(So
mm
vessel
h6 + h7 + h8
=
mm
TOTAL VESSEL HT TAN/TAN
= SSSO
mm
= 2500
mm
PRESSURE
,Max stress
ALLOWANCE
p=
2-5
barg
C =
3
mm
Diameter
I
1000 bar f5
tmin
= D/800
8. Vessel weight f=
7’
L=
6-q
D=2-5
I -2”yo
s=
efficiency
Joint
+ C + 3 mm
Gig.
PxD =ZxSxE-1.2P
+c
E = o.%S
t.85)
=
6-8
=
9
mm mm
6)
mm
Shell
weight
= i=os>o
m (5-9-I)
Head
weight
=
m
(t x D x 20) TOTAL
I
D
:
5 = 1220 bar CS
450
TsoO -
WElCHT =
kg
kg
kg
Sheet
I
I
m-0
PROCESS
CALCULATION
TOTAL
f-moP/MP/
VAPOUR-LIQUID
SEPARATO
EXPIQJR CHK
kiEET
QATE
JO9
TITLE
E’XCTPZQ~
NO JOEI
w
: N-
2 of 2
:
ITEY : pqcc=4 VERTICAL
@iY
mm
thickness
.
I
mm
150 mm for bottom LC 300 mm for side LC
h8 :
7.
mm
0Qo-r
a.3+ :
tZICh-WwC
PEV
CALCULATION
SHEET
HORIZONTAL
FOR
2 PHASE
TAN/TAN (L’) 6530 L= 6000 mm
I-
-c*
4
-1
6i
a
D= Zooo 5. -Dr
Fc
Head type 2:l elliptical/k Indicate on sketch if demister
EQUIPMENT
l
mesh required
w elec Vapoc % ToTotal Liquic
N” : v zo\o
DESCRIPTION
:
Delete as applicable
l
t
Operating
data :
Operating Operating
pressure bara = temperature ‘C =
Gas molecular w+ cgas flow rate Gas density T, P Qg acttial vol flow Gas viscosity
I ”
20
r8
= -*cc = (3 950
Kg/hr Kg/m3=
t%O
m3/s
=
O-Z??
cP
= 0.0toBS
cala Selec L/D ( Flow1 a) Ta
Liquid nature : ~ti Liquid flowrate Liquid density T,P QL actual vol flow
Kg/hr = 121 650 Kg/m3= XS.0 m3/min = 2-65
Particle
microns
size
=
(50
HLL b) VC LLI. V 9b‘c CalC~
1. Vapour-liquid
settling
velocity
or calculated
: from Fig. 1
c=
2. Max. vapour velocity
;
vs
Vm=VsxFxL
=
Vm= O*SVC m/s
flow
Qg =
0.2TI
m3/s
AV = 9g = 0*4X Vm
liH0
PROCESS
TUTAL
CALCULAnON
ml50 ‘EP/DOe/olP/
I
EXP/QJR
1
I
- _ --
m/S
E
L/D T 3 3. Actual vapour volumetric
NOT
I<
CALCULATION
FOR HORIZONTAL . OHfUE - r
m2
.
SHEET ITEM
: EXm-lk~
NO 1nFI
: &I= .
f
4 . Nozzle
sizing
vel limits
inlet flow = o-32\
pi :
Gas exit = O-Z% Liquid outlet = O+
:
6
m/s
inlet
7-13,
Exit
15-30,
liquid
1-3
m3/s
NozzleID=
8
”
Actual
VCI
m3/s m3/s
NozzleID= NozzleID=
6 6
n ”
Actual
vel = t5 m/s
Actual
VCI
= 16.8
m/s
0.35
(+ 10 %I
62
:
= 2*1
m/s
5. Drum sizing vol required
For trial 1 tres = 4 mins
-
elected h/D Vapour area % Total area Vig. 3) Total area Liquid area
m2
Ar Al
m2 m2
Calculatd drum 6 Selected drum P
D
L/D (3 - 4) Flowpath length
L
a) Tan/Tan
L’
length
i HLL height b) VOL Q kLL LLL height ; vo1’3 LLL AVOL ;__ VW ’ Calculated tres i
I
Av
d-e.
= 4 x QL =
m3
to*&
mm mm
-
I I
mm
srso
,
NOTES : SELECTED
DRUM : DIAMETER
b 2000 mm x 65%~
mm tan/tan
I
a)
I$/tan length L ’ = L + 1.5 x Pi + 1.5 92 I nore this correction if D < 1.2 m and use L for volume talcs. For trial 1 use L and ignore heads).
b)
if
VOL HLL is less than required inspection).
RR0
TOTAL mm-/
-
=vDDP/MP/
l a* ’
PROCESS
CALCULATION
FOR HORIZONTAL 2 PHASE
ExP/suFI DATE
r
1 =“((
’
surge increase D, L or h/D or reduce tres (by
Jo8
TITLE
:
CALCULATION
SHEET
lfEY : NO JOB
fX&l+WLC
: N*
:
REV
6. Wall thickness . .
DESIGN PRESSURE CORROSION ALLOWANCE
P= k-q C =’ 3
barg mm
Max stress
Joint efficiency
f
=
PxD
2SE- 1.2P
+c
=
2s
CS = 1220 bar SS = 1000 bar s= I220 E = 0 ~85
mm
8. Vessel weight (Fig. 6) = 2s L = 6.53
t
mm
D=
m m
2
Shell weight Head weight (t x D x 20)
= LO 800
kg
= \ 000
kg CA
TOTAL
WEIGHT=
I?,
000
kg
Wg Del
Qs Par
II II ‘I ‘I mmn
.
TOTAL
CALCULATION
m-mu TEP/DOelMf
I
I
/ UP/
mocEss
t
I
SJR
I
FOR 2PHASE .^_ -.-. -
CALCULATION
HORIZONTAL
SHEET
;
ITEM : NO
:
*nm u. .
EWPLC Ilh=”
TANRAN LENGTH PLOW PATH LENGTH
L
01
L’ - Soeo Lr 4%oo
I I +y2
pt.
0
. Amend sketch if boot required instead of baffle Indicate on sketch if mesh required Heads : 2 : 1 elliptical
EQUIPEMENT A
No : 0 Se\0
B
3400
!
Operating
data :
Operating Operating
pressure temperature
bara ‘C
= 4-0 = 50
CONDENSATE pc
WI
Flowrate -.
Density
QL GAS MW I-
= 4saqt
Wg flowrate Density Q T,P
kg/hr Kg/m3 = 35.0 W-ATER CUT m3/& = 1tq : 0~~3Lq5 pw x o.ocn cQ
Qg Vol flow
P
i Parricie
PC 1x5 i- Yln-:y,rc - -;- .-:
microns = tso
1. Vapour-liouid
settling
velocity
T,P
Vol flow T,P m3/min = 0*‘i1 = 0.75 Viscosity cp w
I.
Kg/hr
Flowrate
= QSsS
Density T,P Kg/m3= 988 Vol flow T,P m3/min = o-168 Viscosity cp = 0-S
QW
size
Kg/hr = ‘3tooo Kg/m3= 32%.4
PW
: from Fig. 1
vs = 0.135
m/s
I or
i.,. mv
2. Maximum
calculate2
c ,=
vapour
velocity 3. Liauid-liquid
L/D = 3
;
vs
Vm=VsxFx& -\Y+. F’ ,,D
=
Vm=
dS
O-rcrc6
m/s
settling
t
Oil in water I Water in oil
u, = 0.513
f--/c Pd El ut = 0.513 p-/c
mm/min
HPC
I
mm/min
.‘. &oil
=
-*. Utwater
2lJ
mm/min
= \7+5
mm/min
I -I -’
SI;u
TOTAL mm
PROCESS
CALCULATION
CALCULATION
FOR HORIZONTAL 3 PHASE
SHEET
I
ITEM : NO
:
C%4w+d
4.
Nozzle
sizing:
vei
m/s : inlet
limits
m3/s 1. Inlet
flow
7-13,
Exit 15-30, liquid nozzle id :
:
1-3 actual
vel ,M/S
1
:
(+ 10 %)
2. Gas exit : 3. HC outlet : 4. Water outlet :
o*oss
L”
o-036
6.
0 ,012
3”
0 *002B
(IO0 -1
ci*%
6.4 (w-1
2.6
3”
0.G
,
A
5. Vessel sizinq For trial
1 use hold up time
oil (HLL-111)
= 4 mins
-
2-W
n’
OIL SECTION
Selected h/D Calculated (Qg/Vm) Av as % AT (Fig. 3) Total area Liquid area
Av
m2
AT AL
m2 m2
Calculated fJ Selecred 0
D
mm mm
L/D (3 - 4) Flowpath length a) Tan/Tan length
L 1’
mm ‘mm
hl
m 11: m3 mm m3 m3
I
HLL height VOL at HLL LLL height VOL at LLL AVOL Calculated
h2
1 650 1 1000
I 19
1srt500
1250
-
min
tres
Notes or comments : .
a)
tan-tan
1engthL’
= L + 1.5 x (61 + 62) mm - Ignore if D < 1.2 m
PROCESS’ CALCULATION
TOTAL ~/orPfDw/uP/sm erl I i34K
CALCULATION
FOR
HORIZONTAL
3 PHkFE DATE
\
JOB
TITLE
SHEET
‘.
-I
2
ITEY : lridA4Pd
MO : :
.. . .
JOB
Ma
.
SIFV
i
+ 1I
% ATER SECTION Trial
I;
1
B = 2/3 x L =
mm (rounded)
3450
Total liquid vol flowrate Qw + QL
I.
m3/min
B Baf fie distance AL Liquid area at HLL Vl Horizontti vcl at HLL Ut water (step 3) Vertical fall from HLL = B x Ut/V Final settled h = HLL - vert fall
I, I I I
Liquid area at LLL Horizontal vel at LLL 1 Ut water (step 3) Vert fail from LLL = B x UGJV2 Settled baffle height Selected HIL level (adjust h3 and B if necessary)
:? mm/min mm/min mm mm
AL V2
h3 h4
1 1 1 I I I I I 1
3460 o-s34 ‘OS5 I??-S
I
0443
I WI5
mm mm mm
; 290 1 400 I 320
mm/min mm/min
I ZW
mm
I
I
I
I I
t I
I I I
i
I I
I I I
I I I I I I I I I I I
i
I -w I 1 400
mm
I bo
ql water vol at HIL (upto baffle)
m3
1 I-O! i
’ m3
1042
q/Qw time q3-q4/QW
I I
I I
mins
i
3
CMK
DATE
JOB
CAiXULATlON
FOR HORIZONTAL PHASE
Ep/DoQ/Dw/ExP/sufl BV
TITLE
i
:
I
I I I I
i
I I
I
t
PROCESS’
CALCULATION
I
I I
mins
.
mm2 TOTAL mQ3
I
I
1 Vol (NLL - NIL)/QL
I I I I
I I I I I
I
I I I I I
time (upto baffle)
I I I I
I
I 1 2-h
m3
q surqe = vol (ql - q2)
I
I I I I I I I I I I I I I I I
1
t
1 2.3
m3
oil residence
i I
mins
q4 water vol at outlet ( ” 1
calculated
I
I I I
m3
residence
I
I 1 oar 1 I Oti I 10.3 I
$3 water vol at NIL (upto baffle)
surge time
I I I
I I
I
vol at LIL (upto baffle)
/ I
1
1 1 ZTO
h6 selected outlet height
q2 water
I
I mm
I I I
I
*to
h5 selected LIL level
t
I
f I
Check oil rise : Horizontal vel at LLL v2 Ut oil (step 3) Vert rise avec dist B = B x U+/V2 = mm outlet height
I 1
I
s2=
m2 mm/min mm/min
I 1I
I 1I
I I 0.88
SHEET
3
-
ITEY : Elc4tiPti NO JOB
: Ho
:
REV
TEP/DI
6.
Wall thickness .
DESIGN
PRESSURE
.
CORROSION
ALLOWANCE
P = u-7
barg
C=3
mm Joint
t
8. Vessel weight
=
=
PxD +c 2SE- 1.2P
(Fig.
6)
Max stress
CS = 1220 bar 55 = 1000 bar
efficiency
35
s=
I220
E=
.8<
mm
#,
,:. I ..
:
?26/0
t= 35 i=S
mm m
Shell
weight
=)&>-kg
Head
weight
=
D = 1.5
m
(t x D x 20) TOTAL
WEIGHT
,
LOSo
kg
=
’
b
PROCESS
FOR HORlZONTAL 3 L’HASE
CALCULATION PI-IMP/ v
EXP/ PYY
SaJSUR
CALCU
ILATION
SHEET
4
.
ITEM : Ad., E%qv\. NO
c
:
-OATE
9
TITLE
:
JO8
N’
:
1
REV
rb
TAL T&P/DP/ExP/SUR
I
PROCESS
ENGINEERING
DESIGN
I Revision
MANUAL
:
0
Page tuo :
VAPOURANDLI:QUTDSEPAR&~RS Date FIGURE
VS - LIQUID
SETTLING
1
VELOCITY
nd
: 2/85
2.20
PROCESS
ENGINEERING
VAPOUR AND LIQUID
DESIGN
MANUAL
Revision
:
0
Date
: 2/85
Page NO :
SEPARATORS
TkP/DP/EXP/SUR FIGURE 2 DRAG-COEFFICIENT VS Re or C (Re$
(Cl
O@
N z
a 0
2.21
Page NO : TEP/DP/EXP/SUR
1 I FIGURE 3 ..____ RELATIONSHIP BETWEEN CHORDAL HEIGHT AND CIRCULAR SEGMENTAL AREA
0 a w 0
0
5
10
15 PERCENTAGE
20
25
--
OF ClRCLE DIAMETER
--
4
rOTAL
PRWESS
ENGINEERING
DESIGN
VAPOUR FND LIQUID
MANUAL
:
0
Date
: 2/8S
Page No :
SEPA!!TORS
TEP/DP/EXP/SUR FIGURE
Revision
2.23
4
3 PHASE ALL
SEPARATOR DIMENSION
SHOWN
ARE MINIMUM
RECOMENDED MIN
UY
300
mm
min
HIL -------
+&y
,M)-
1,
100 -I-lm
OIL RESIDENCE
-
TIME
Volume
150
between
use residence
OIL SURGE
-
TIME
Volume
use 4-5 minutes
WATER
RESIDENCE
TIME
-
Volume
SURGE
TIME
-
Volume
upto
HLL and LLL.across
full
if feeding
column/vessel
to another
3 minutes
if flowing
8 minutes
if sole charge
between
NIL and outlet
Use 4-5 minutes
only
for design
if pumping
between
baffle
of 3-6 minutes
5 minutes
Use 4 minutes
WATER
NLL-NIL
time
between
fg
minimum HIL and LIL minimum
length
to storage to storage to fired
(no pump)
heater
of vessel
TE
‘age No :
,Y, “‘VOTAL
PRbCESS ENGINEERING
DESIGN MANUAL
Revision :
0
Page NO
VAPOUFt AND LIQU,ID SEPARATORS 2.23
TEp/Dp/EXO/SUR
Date
: 2/85
FIGURE 6 Vessel weight estimation
u t of two heads = B(m)xt(mm)xZOKg
fIE 2.400 t-200 _.~ 1.900 1.600
From hydrocarbon processing August 1981
T iFI o i
1.400
12UO
essel
1.ooo 900 600 700
I
600
so0 I
1
IAH!
s
6
7
8 910
12
oddlmlokl+c c08nNl sdcns Jwt" I I IIlrlll I 1416162024683025404560
I
IL
t Thickness mm t’
L
t FEED
’
min of 1 l/2 x nozzle 0
GAS OUTLET HLL
t
L
S~TANDPIPE OIL EXIT NOZZLE
WATERDRAIN FIGURE 5 3 PHASE SEPARATOR
WITH WATER BOOT
2.24
:
TABLE
. FOR
GAUGING
HORIZONT+L .
Cjod - Pct.ccntagc
of Total
2
CYLXNDRICAL Diayctcr
0.0053 0.0152 0.04L9 0.0788 0: 1tlL
0.4
.
0.6 0.8
1.0
0.1691
1.t 1.4 1.6 1.8 L.0 , L.2 (..4 /,.6 a.!. 8 3.0 3.2 3.4 3.6 3.8 ’ 4.0 4.2 4.4 6.6 . 4.8 5.0 -* 5.2
7.6 ;
.li
;’ 8):’
:.
7..8
;
8:C! 8.L
./
.O.LLL3 o.reoo 0. Ml9
4.3131 4.456L 4.6045
9.6 Y.8 10.0
4.9015
0.4077
0.4773 6.5501 0.6~63 0.7061 0.7086 0.874L 0.9GLS I’ . 0533 1.1470 1. L43L 1. 3418 1.44L? 1. 5461 1.6515 1. 759d . 1. e693 1.8914 2.0756 .~.2116 L. x97 L.-I497 2:57 15 L. 6951. L.&L11 2.9493 3.0771’ 3.2082 3.3408 3.4744 . ‘3. blot, 3.7460 . 3.8865 4. X76
4.75L5
5.05L3 5.2040 5.3580 5.51LL 5.6690 5.0258 5.9848 6. 1445 6.3060 6.4665 6.63~0
11.6 11.8 IL.0 1L.L lL.4 Id.6 I/..8 13.0 13.2 13.4 S3.6 13.8 14.0 14.2 14.4 !4.6 14.8 15.0 15.L 15.4 15.6 15.8 16.0 16.C 16.~ 1C.C lb.6 17.0 Ii.2 17.d
6. *i970
6.9630 7.1305
7 .t990 7.4680 7.6390 .7.811G 7.9840 8.1580 8.3330 8.5090 (3.6360 8. e645 9.0440 9. EL40 9.4050
9.5880 9.7710 9.3560 JO. 142 10. 32-i 10.515 10:;03 10.893 ll.O& 11.273 Jl.-I65 11.657
l’
17.6 17.8 18.D 18. L 18.4
IL.437 . IL. 633
18.6.
1L. 831
18. 0 19.0 19. L 19.4 - 19.6 19. 0
13.030 l3.‘Li9 13.4L9 13.630 13.832 14.035 14.L38 14.444 14.649 14.854 15. o;jo 15.267 15.375 15.663 15.89L 16. 101 16.31~ 16.5~4 16. ‘137 16.9~9 I?. J6i 17.376 l 17.590 17.806 18. OLL’ 18. L40 18.457 10.675 18.891
11.851 1~. 046 12. L40.
LO.
0
LO. LO. /,o. LO.
2 4 6 8
Ll. 0 Ll. L Ll. 4 ~1.6 21.8 LZ.0 Lt. L ‘2.4
LL.~ LL.
8
L3 0 23. L L3.4 ~3.6 23.8 24.0 L4.L
L*i. ~4.6 L/r. LS. /.5. 26. Lb. L7.0 it.
4
19.110 8 0 5 i; 5 5
19.330 l?.S.sl LC. iOh 1.3.061 r: 1. LLZ ~1.785 LL.‘JS3 ZL. 923
ENDS
of Total of Tank
L8. 5 L9.0 L9..5 30.0. 30: 5’ 31‘0 31.5 3.:..0 31.. 5 33.0 33.5 34.0 34.5 35.0 35.5 36. 0 36.5 371. 0’ 37.5 38.0 38. 5 39.0 . 39.5 40. o40.5 4J.G’ 41.5
;g-;
43: 0.
Capa
L3.49 24.07 L4.65 LS.L3 25.81 d6.40 ~6.99 L7.5E L8. 18 ~8.78 d9.30 L?. 98 30.58 31.19 31.00 3d.41 33. OL 33.63 34. LS 34.67 35.4s .36. 11 36; 7’ 37.35 3i. 9t 58. 6C 39.2: 3?. 8t 40.4’.
41.1; 41.74 42.31 43.0 43. 61 44.2; 44.3 45.51 46. 11 46.8
43.5. a14.0 44.5 * 45.0 4’5. 5 ~6.0 46.5 47.0 47.5 -:a. 0 4b. 5 43.0 * 49.5 50.0
17.4:
~8. C’ 48. 7. 49.3 50. f
1'1 LCI. is;:0 CL1 I;Y. * Cl \Y, F. C!:r::,Ic' 2 2 4 ': fTj ;t.,* N '/ -,7.-y l~c),' r G5/.9.~~~ -.-..-..-.-.--.--I-__..._...----.-... --IL.-Y-. ..-I#--.D - -v--y---8.6 c.4
.--.-.-.-em-1*.:1
a*#.::,
.,
6.16’36
I(‘,
------_-_-.-.--_---.-. ;.,*r:,
c’-yr-7’
,
I
8.8 9.0 9.L 9.4
10.2 10.4 10.6 10.8 11.0 1 l.L 11.4
- FLAT
- IdC - PcrccnLa8c t
of Tank
0.1 0.2
TANKS
-
i
iE. G
-.I_.----v.I
/-
;;*.
-
DF’C
-.-.-*
--.
Aker Engineering plc D
c I
I -_..i
.. I
--8G
I I t , ,
_.-__
:
1. .--: - .,..--. -..-__-_---1 -_ _ ..-. 1.--.. I-+ ) I_ 1 , .--.- ..-.-
-._‘; , ---.---., .--_ ._-7f
I
-.--
I
-.-.--
__--
-
, I
65
___-_
_
_--.
.
__
__.-,
.._
.--
60
I
+I
J-._..
I -I--I. i ! iI _-. I-.-- - _ __ __._ _ I I --
-.
__
II --+---i--I
I I .r..
---.: /“--
_A---.
7
l
-----
- : -_.-
I I -. Ii II .A.-
-.
.._ I
---I
I1-._._ I
-- i-- --I--I I
-0
5
10
/5
20
&‘;s’
30
PL-&?CENTACL-
35
40
OF
46
50
C/h?CLE
55
60
65
D/AMETE~
-.-
---
-.7b
75
60
85
so
95
Ioc
‘TOTAL
PROCESS
ENGINEERING TRAY
TEP/DP/EXP/SUE
1.
DESIGN
MANUAL
COLUMNS
Revision
:
O
Date
: 2,85
Page NO :
3.1
APPLICABILITY .
It
expected
is not
performed
column
Should,
however,
sizing
of hand for
mechanical
on glycol
towers
design
AND
for is given
of a tray
height
trays
column
be
require0
any
or similar.
be required
is the
in Section
column
srudy
simulator,
and
valve
absbrbtion
or pre-projecr
diameter
calculation
or
SSI PROCESS
tower
method
distillation
of a feasibility using
of
this
see package
DESCRIPTION
of a tray
be performed
estimation
of the procedure
,4 detailed
2.1.
would
methods
calculation
For the purpose
a quick
common
example
2.
a hand
by the engineer.
rigorous
most
that
“GLITSCH
one
of
the
METHOD”.
An
3.
is beyond
the
scope
of this
guide.
For
details
units.
NOTES
TRAYS
There and
are valve
basically trays.
Each
criteria.
process
Bubble
three
types
type
Some
used
has specific
of the
major
in distillation
applications aspects
columns
and
are
; sieve,
flexibilities
detailed
bubble
dependant
as follows
cap on the
:
caps
Operation
Vapour
:
the
passes
Capacity
:
Application
:
high
many
Note
: most
All
major
IS” is normal.
on
tray.
the
liquid
tray
most
Consider
action
tray
bubbles
effects
via
outlet
intc liquid-
weir
ant
50 %) is maintained
at varying
head.
common are
type
of
available
tray-consequentI>
from
vendor
sources.
of tray.
excepts
flooded
cap then
below.
liquid
type
Ideal
the
(minimum
the
bubble
Bubbling
tray
efficiencies
expensive
the
exits
to the
was
services . conditions.
remain
into
maintaining
years
published
“risers”
efficiency
due to weir
many
must :
The
,Moderately
fouling
spacing
contact.
arrangement
For
:
liquid
downcomer
rates Efficiency
through
surrounding
vapour
Tray
of tray
coking, for
use
to maintain 24”
polymer in low
formation flow
a vapour
to 36” for
vacuum
conditions
seal. conditions.
or other
higt
where
tra)
.
1 TV ‘@
pROCESS
TdTAL-
ENGlNEERlNG
.,
DESIGN
MANUAL
:
Date
2/sr
Page No :
0.
TRAY COLUMNS
TEP/DP/EXP/SUR r
Revision
3.2
Sieve trays With downcomers Operation
:
Vapour
rises through
holes
and
bubbles
liquid.
liquid
flows
over
weir
via
Without i/S”
to I”
Vapour
through across
and
tray
downcomer
rises
through
bubbles
Liquid
to
downcomers through
head
holes
to
tray
generally form
in
liquid.
forces
liquid
through
same
countercurrent
tray below.
holes
below.
random
Flow
is
and does not
continuous
streams
from
each hole. Capacity
As high
:
down
as or higher
to
60 % of
performance
than
bubble
design.
is poor.
At
Generally
cap trays
lower
for
rates
design
efficiency
unacceptable
rates falls
or and
to operate
below 60
Efficiency
becomes
% capacity. Efficiency
:
As high
as bubble
unacceptable variable Application
:
caps a< design
below
60
% design
capacity.
Not
suitable
rates
are
for
load columns.
Systems
where
maintained
high
in
particles
well,
capacity
continuous flushing
plug.
Not
near
design
service.
them
to run with salting-out may
capacity.
Handles
down to tray
systems
recommended
where for
oil
suspended
below.
trays
to
be
solid
Can be problem
run hot and dry, holes
+ gas service
due to poor
flexibility. Tray spacing
:
15” average,
9” to
table.
20”
Use
12” accep KO 30”
for
vacuum. Valve rravs/ballasr the
proprletry
design Clitsch,
distillation
9” to 18” accep
table.
18”
Use
to
30”
for
vacuum.
cao
Generally include
12” average,
same
aspects
for specific Koch
as for
sieve
operation
(flexitray),
trays.
problems
Nutter,
Union
Most
valve
and capacities. Carbide.
trays are speciaiist Specialist vendors
Best
choice
of tray
for
application.
Tray layouts Not
only
may
the type of bubble
design but also the tray hydraulics in Figure 1.
cap/valve/sieve C.
liquid
path.
hole be specified Common
for a particular
arrangements
are shown
^“-
rOTAL
PROCESS
ENGINEERING
TRAY
TEP/DP/EXJ’/SUR
DESIGN
MANUAL
COLUMNS
Revision
:
o
Dale
: 2185
Page No :
3.3
Trav efficiencies General
tray efficiencies
t
to use :
Absorbers Hydrocarbon Amine
oils + vapour columns
%
Hydrocarbon
oils + vapour
towers
usually
5C-8C b
15-20 %
(Amine
have 23 actual
GO-80 %
trays)
installed
on the
overhead
internal
tower
reflux.
Design
exist,
partial
and total.
CONDENSERS .
Condensers
.
are
usually
recover
liquid
covered
in shell + tube exchanger 1
Basically
two types of overhead
total
product
condenser
vapour.
For
and provide
portion
a partial
equilibrrum
condenser
point
is split
vapour
the returning
reflux
tray.
fractionation
towers
to
of condensers
is
When using
heat of the saturated with
some returning
a
overhead
as reflux
and
product.
the
additional
to the latent
liquid
as distillate
condenser
with
an “external” control
bubble
of
section.
the heat load is equal
The resultant,
the remaining
2.3.
35-50
units
Distillation 2.2.
Strioping
The
withdrawn
the
and consequently vapour
with all or part of the liquid
from
the condenser
is normally
returning
accumulator
withdrawn
as reflux
is In
is acting
under
as
pressure
to the column.
REBOILERS Generally
.
three internal
reboiler
external
“kettle”
type
external
“heat
exchanger”
In most .
The
Reboilers medium
.
Values methods
exchanger
type
hydrocarbon
should
be heated
furnace,
type is preferred
exchanger”
so that sufficient may
exist for light
fractionators.
thermosyphons
cases the “heat
heat
column .
types of reboiler
be located
head is available by direct
fire,
electrical for efficiency.
2-3 m below
the exist
for thermal
circulation.
nozzle
electrical
coil,
steam,
for various
types
of reboiler
from
closed
the
heating
or process fluid exchange. of ti overall
(incl.
fouling
factor)
are given in the heat exchanger
design
guides.
and desrgr
siq----
PROCESS
TRAY
TEP/DP/EXP/SUR
3.
DESIGN
MANUAL
Revision
:
Date
: 2f85
Page No :
0
COLUMNS 3.4
CALCULATIONS See following
4.
ENGINEERING
pages :
REFERENCES 4.1.
AND
3.5
USEFUL
to 3.11 LITERATURE
Distillation Part
I :
Distillation
Part
2 :
Hydrocarbons
Parr 3 : 4.2.
Absorption
4.3.
Gas liquid
4.4.
Thermosyphon
Mechanical
Process
Performance
Absorption Designs
and fractionation
8
+ stripping
fundementals
CAMPBELL PERRY
piping
VOL II - CHAPTER
for Performance
systems reboiler
LUDWIG
design 1
VOL I - CHAPTER
- CHAPTER
W.F. ABBOTT - Hydrocarbon
TRAY
TYPES
18 MOBIL
Pr. March
BY
FIG.
LlQUlO
1
1982
PATHS
13
No :
3.4
TRAY
CALCULATlON
Column
?>
item:
Tray number:
SHEET
Zo(6
8
VAPOR
I.
DATA
Number-of
passes:
2
TO TRAY
kg/h
/
MW
)
kmol/h
1
k
I
PC
I
I I 13-n
‘C
m
=
T,.
= t,
+ 273
=. 2.86.1+
T,
= tc
+ 273
=
T,
=
P 308.7
PC =
K
Then Z =
Dv
4842
P,
= p
O-637
\
Tc
Vapor
ATM.
abs
ATM.
abs
K
L 0.522
1-1
23-6
=
t 0~S-f PC
density 12.03x
=
kfw
x P (atm)
12.03 x 31.4 x 27.6 3.63;LI x 286.(3
=
z x TV (‘K) =
actual
c, = kg/h Dv
I- - i-
‘-.
=
kg/m3
, - * ..,,
t
Vapor
53.806
5:
rate
=
16%%0
=
m3/h
53.806
Sheet
HS
PROCESS
RIU TOTAL mE0 EXPf
TEP/DU’/DtPf
&BY
CHK
CALCULATION
NO DATE
1 JO8
:
COLUMNS
SUR TITLE
:
4
SHEET ITEY
TRAY
1 of
JOB
t%4fvu
: N*
:
REV
2.
LIQUID
FROM
tL
13.2
=
lC
d@lj
= Oe38q
Liquid
flowate
CL
3.
=
TRAY
dL at tL
kg/l-
= O-411
kg/m3
x IO3 =t”
or
kg/h
= 7 b ooo
kg/h dL at tL (kg/l)
98000
=
@
=
DOWNCOMER
DESIGN
VElOcrrY
TS = 1%’ =
650
mm
DL - Dv =
3.9
kg/m3
VDdsgo
3io
mJ/h/mz
238.4
m3/h
-.
41i
at tL
“hsg ..
4,
=
System
factor
“Ddsg
= “Ddsgo
VAPOR
CAPACW
TS =
4SO
CAF o = System
CAF
Kl
6.
APPROXIMATE
1
x KI
=
FACTOR
maxi)
\ )
mJ/h/m
32
-
) (610 mJ/h/mZ
d (Tabie
2
CAF
0*‘58
= CAF,
VAPOR
(Fig.2
SPerJc,
mm
factor
5.
=
Tiiy
(Fig. 3 1
K2
=
l.0
x K2
=
EFFECTIVE
(Table
x 0.38.
1.0
LOAD
COLUMN
,2) =
0 a38 -
V Load
DIAMETER
DT
= 2.5
m (Fig.41
.
Sheet mu0
.
*
.
PROCESS
TOTAL
no
~~fllwf 7
EXPf SUA CHU DATE
CALCULATION
COLUMNS NO
JO8
TITLE
:
4
SHEET ITEY
TRAY
2 of
Jo8
:
EXA4CLC
: N*
:
REV
COLUMN HEKHTESTIMATION
3.2.
Ql
a.
H
See design details
:
Minimum inlet
distance
nozzle
on vertical
for,Hl
vapour-liquid will.
separators.
be one tray
spacing.
Minimum
distance
between
and to tray 300 m. Selected
HI =
600
mm
b. H2: HZ : tray spacing No actual for
?
x (number
of actual
trays = theoretical
see section
2.1
trays/
trays - 1) 7
56%
=
Actual Note
: if the column h, = r z(01 2
diameter
changes
over the length,
- 02) long and HZ will
increase
fzs-rr ti&-rC
l6
trays = the transition
piece will be
by this amount
Selected
HZ = 6
?SO
mm
Sheet
mm2 TOTAL mHl
PROCESS’
CHU
ITEM
JO8
TITLE
:
4
:
EZ(G4QLE NO
DATE
of
SHEET
TRAYCOLUMNS
EP~WP/DIPIEXP/~SUR BY
CALCULATION
3
JO8
: No
REV
/
c.
H3:
H3 = hl + h2 hl = tray spacing
Qao
x 2=
h2 - see vertical
separator
*m
sizing
.
= h6 + h7 + h8 Ser
h6 = hold up time
volume ,X0:
For production
flowing
to :
Flo IV0
.
another
.
storage
I
a furnace
.
another
.
reboiler/heat
t
column
= 15 min
He
2
Set
10 5
unit
5
exch. .
h6 =
2000
h7 =
h8 =
coo
‘500
SE H3 = hl + h2 = 3-0
mm
ii
Selected
H3 = 3Wo
F
mm
tv ts
TOTAL
COLUMN
HEIGHT
= Hl
+ HZ + Ii3 = 6750
mm
Sheet PROCESS
roTAL P/DoefuP/uP/mm
TRAY
COLU:
;Us
CALCULATION
SHEET ITEM : MO:
4 of
cuT+fLc
4
PROCESS
ENGINEERING TRAY
TEP/DP/EXP/SUR
DESIGN
MANUAL
COLUMNS
TABLE SYSTEM
Revision
:
Date
: 2/85
3.9
1
FACTORS
l
System Factor
jewiCe
\ion foaming, Fluorine
systems . . . . . . . . . . . . . -- . . . . . . ..I.~.................~.........~...~....
regular
1.00
e.g., BF3, Freon . . . . . . . . . . . . . ..-.......-..........-.-...................
systems,
Moderate
foaming,
e.g., oil absorbers,
amine
and glycol
0.9 .85
regenerators......
absorbers . . . . . ..-.......I-.................. Severe foaming, e.g., MEK units . . . . . . . . . . . . . . . . . . . . . . . . . . . . ..-.....................-...... . . . . . ..-......-.-............-....... Foam-stable systems, e.g., caustic regenerators *eavy
Page .No
foaming,
e.g., amine
.73
and glycol
.60 -30 I
1
TABLE SYSTEM
2
FACTORS System Factor
Service
Non foaming, Fluorine
systems .............................................................. e.g., BF3, Freon ........................................................
systems,
Moderate
1.00
regular
foaming,
e.g., oil absorbers,
amine
and glycol
regenerators
0.9 ......
.85
...................................
-73
Severe foaming,
-60
Foam-stable
e.g., MEK units ........................................................... ..................................... systems, e.g., caustic regenerators
-60
Heavy foaming,
e.g., amine
and glycol
absorbers
TABLE Column
diameter
3 1Minimum recommended Tray spacing : 75 mm
mm
0
<
1 200
450
1 200 <
0
<
2 500
600
2 500 <
0
<
4 200
700
0
>
4 200
’
950
TOTAL
PROCESS
ENGINEERING
DESIGN
MANUAL
Revision
TRAY COLITIS
TEP/DP/EXP/SUR
Fiq.
CAF,
c -
-
-
-
-
-
I --
7
FLOOD
CAPLCITV
OF
IALLAST
TRAYi
:
0
Page No :
PROCESS ENGlNEERtNG No :
10
-
-
TRAY
DESIGN
MANUAL
Fl9.
-
:
Date
: 2/85
~~LwQIS
-Ep/DP/EXP/SUR
(FOR
newwon
tauLAsr APPROXIMATION
w
rage No :-
3.11
TR*v DIAMETER PURPOSES
ONLY) lrl’,b
Ll0Ul0
. ”
LO40
m’*m -
-
100
3000BASE
TS = coo FF I IO\
-
-
750
-
700
-
650
-
600
-
Is0
-
so0
-
AS0
-
A00
-
as0
-
100
-
2so
2500
-
-
200
-
'SO
c
100
-
-0
so
OTAL
PROCESS
ENGINEERdNG
DESIGN
Revision
:
0
Date
: 2m
Page NO :
TOWERS
PACKED
TEP/DP/EXP/SUR
MANUAL
3.12
1. APPLICABILITY FEASIBILITY
STUDY
Pat
: PRE-PROJECT
15Under
normal
circumstences
based on process
data
supplied
complex
and requires
transfer
data for the fluids
For the purpose towers, The
specific
information
of the
by the
A detailed
unnecessary
for feasibility
would
The detailed
regarding
both
be detailed
design
packing
of packed
type
co1
by a vendo towers
i GOI
and size and mas
wit tov
guide details
are given on the general
and loading
height
engineer
references).
tower
contacted.
types of packing
determination
of a packed
by the engineer.
of this design
various
determined
the design
and pressure
of a packed
if required
description.
using
is beyond
and pre-project
tower the
of packet
drop correlations.
should
methods
arrangement
scope
by a vendor
in design
of this
Lit
ant
be evaluated
outlined
,
guide
literature
o (set
and is normall:
level.
In do en
Fc 2. PACKED
TOWER
A general
DESCRIPTION
arrangement
+ NOTES
of a packed
pa
tower
is shown in Figure
1.
Packing The correct required
selection
process,
of a tower
flowrates
packing
and pressure
will normally drops stated.
be made Details
by the vendor
on packing
based on th
i) II
are given in : ‘*lu I\
Table NOTES .
1 - Packing AND
Carbon depending
.
Towers expensive
service
applications.
V
GUIDELINES steel
towers
may
on the nature are generally and gives
types will be stacked
be lined
of the fluids loaded
for being
by dumping
inferior at vendor
liquid
corrosive processed the packing
distribution
request.
service
with
rubber,
plastic
or brie
and the temperatures
encountered.
rather
than stacking.
Stacking
is mor
pressure
Certain
packin
but smaller
drop.
Nc
!
3.i
&AL
/
ENGINEERING
1
heights
column
MANUAL
I
per support
plate/grid
15-21)’ (4.5 - 6 m) for other ‘enc
DESIGN
PACKEDTOWERS
TEP./DP/EXP/SUR
Packing
PROCESS
diameters
packing
should types.
not exceed
Individual
12’ (3.6 m) for Raschig
bed heights
are normally
of
rings
limited
to t;
or 6 m maximum.
‘en m;
ack
Good
liquid
distribution
over the packing
within
the bed. The streams
towers
with D < 36”. For larger
Liquid
redistributors
and 5-10 stacked
diameters packing
of liquid
should
towers
should
be installed
for other
packing
as the downward
is necessary enter
the number after types.
liquid
to promote
adequate
the bed on 3” - 6” square of streams
should
phase contact
centres
for small
not be less than (D/6)2.
approx.
3 tower diameters for Raschig rings Redistributors are not generally required for
flow is vertical.
for ! (5 mal
In order
to reduce
down or floating enough
ceramic
bed limiters
and&carbon
packing
are installed
breakage
on top of the packing.
to hold down the bed and be able to resettle
For ,plastic
or metal
packing
occuring
the bed limiter
during
flow
The limiter
surges hold-
must
be heavy
as the bed moves.
is bolted
in place
and does not rest
on the
packing.
In tl
Packed
towers
Packed
tower
are not recommended should
i)
small
ii)
acids or corrosive
iii) highly
columns foaming
be considered
with 0 < i ft liquids
liquids
iv) low hold up times v) low pressure
brrc td. mor ckin
drop requirement
for
dirty
in preference
service
fluids
to tray towers
nor for for :
glycol
dehydration.
.,
f&CESS
ENGINEERJNG
DESIGN
MANUAL
Revision
.
:
..
.I
Page No : 0
TEP/DP/EXP/SUR
fRAY
COLUMNS
Date
: 9r/a5
4. REFERENCES 4.1 Applied
A&D Process
Design
Petrochemical 4.2 Design
plants
Information
Bulletin. 4.3 Tower
USEFUL
LITERATURE for chemical
+
LUDWIG
- VOL II pp 129-239 for Packed
Towers
NORTON
Co.
DC- IL Packings
Packed
Tower
Bulletin Internals
*I
TA-80R
Hy-Pack Interlox
TP-78 ”
1,
MY-40 saddles
CI-78 .
4.4 Design Packed
Techniques
for sizing
Towers
4.5 No mystery
- John S;- ECKERT Chem.
in packed
bed Design
Eng. Process
Program
Packed
Towers
4.7 Packed
column
Calculator 4.8 Packed
for Designing
on a Pocket
Eng. May 5 1980 T.J.
Chem. Columns
Aug. 24 1970
V.I. PANCUSKA Chem.
Design
1961 VOL 57
John S. ECKERT Oil and Gas Journal
4.6 Calculator
Sept.
Perry
HIXSON
Eng. Feb. 6 1984 Chemical
pp 18.19 +
Eng. Handbook 18.47
3 11
dc
,F-. TOTAL
1 PROCESS
tNGINttHINb
UtSlCiN
MANUAL
nevlrron
Date
Pockirq
FIGURE
hh( -rJ
towrc~ioa in!0 BoUon
RvDirMibrtaf
: 2185
3.15
1
for frctim
Stocked Layers of Lorq8 and (a trrmrdiai0 Simd Pockiaq
(Not Nrcers#ril Sam 0, Balk 0
Packing Puk& h&Ad Glazed and unglaed. Ponxhin Or Chemical stasennz
Page &‘o
Support Flonq0d
Liquid
u I
TEP/DP/EXP/SUR
Liquid
:
I
~kctinq
Suvia
aq--=-
Suppor(
P0cLirq Sohct0d br Procwa opfi(ti loumM0
Appliation
ucnurb
Ncuual didofu %WJ~
axd acid muexcept 0olvcntr.
hybP
Not m hoc, ausuc (&me 70’ P.)
Uoglsxcd
usual
rypspeikda-
aept rpcci81 reqnircnlmt of bow acLsorpcion on surface. special ccnmicr
available
TABLE
1
for
mild curtie zzy*
Par-
PACKING SERVICES AND SIZES
a1oDcwuc.
St an
rho&
d
Thcrmrl low cubic
weigh
light
weight
Packing Sire This affects contact efiicicncy; usually, packing is more efficient; however, pressure
the
rma’ drop
ClY.aSU.
As a gmeral Packing
guide,
Size. Nominal, **- 34” $# _ 1” 1,, - 1%” 1%” - 2” 2 ,, - 3”
use:
inches
Column
Diam., inch 6 I, - 12” 12” - 18” 18” - 24” 24” - 48“ 36” - larger
TOTAL
PROCESS
ENGINEERING PACKED
DESIGN
MANUAL
Revision
:
Date
: 2/85
-RS
TEP/DP/EXP/SUR
0
3.0
iDesign Techniques for Sizing PackedTowers Reproduced from NORTON 'resign Information for Towers ' Bulletin DC-11
100
Paw No :
3.16
. ..-
.
_
GBEWLEDPRESSUREDAOCI’
L
7
1. Tc tr a1 ba
.
. 1 2. * P J
IC (a d h J
n c s c C
Packed
i t I I ‘ I I
I
002
0.04
06
0.1
02
0.4
1.0
0.6
2.0
4.0
6.0
/ i
t-/E--
Packing Factors (DUMPED
PACKING) Nominal Packing Size (Inches)
Packing
3
Mat’l.
Type
lt6
‘/r
‘A
Va
‘A
loril
1%
11/i 2or12
3
3’/ior#3
Hy-PakTU
Metal
43
18
Super SaddlesIntalox’
Ceramic
60
30
sutydfdlrl:,lox
Plastic
33
21
16
Pall Rings
Plastic
Pail Rings
Metal
lntalox*Saddles
I
Raschig
Rings
Ceramic
Raschig
Rings
5/32” metal
Raschlg
Rings
‘/6’ metal
8erl
Saddles’
P8Ckllle ‘OJtJ
fWtO’t% by LJ”J
725
I Ceramic
’ 1600
Ceramic det.“lW,ed
rtt,,
JWrJtJl
52 (
40
24
16
70
48
33
20
16
145
92
52
40
22
125 95
65
37
110 83
57
32
65
45
200
1000
580
380
255
155
390
300
170
155
115
410
290
220
137 -----I
170
110
240 1
900 J”
97
330
700
SfltJ”l
In M’
1.0.
15
t-r. --
‘I
TOTAL
PROCESS ENGlNEERlNG PACKED
DESlGN MANUAL
a packed Wr. fiat it is necessary to know Of lipuld or gJs IO ba handI& JtId from thas the liquid-gas nuo (L/G). The Oensrt~es of and ftas should be known and the term
--Kf L
2. After
using
-
,I akulatad. tncn the JblOSY. x = - L - is G v- R
alculatlng
for tmven oocrrhng packed towers are
at
not
htgher ownted
pressure aowe
CG’FVO-’ -
EG?--RI
G =
The value of all variables of the Ilqutd. the packmg
I
6 known except for the WsCoslty factor f and the gas t-ate c. The viscosity of the hqu~d can be detemlned from htenture. experiment or l pproxrmatton. The packmg factors Of alI SUes of packmg are gtven tn the table on page 4. grOad(y Speaking. packings smaller than 1 rnth SlZe Jre Intended for tuweo one foot or smaller tn diameter. packrngr 1 mch Or 1% mch m saze for tower over one foot to three feet (0.3 to 0.9 meters) rn drameter and 2 or 3 inch PaCkrngS are used for towen three or more feet (0.9 mere-l In okaml ter. The destgner should select the omoer srze of PJChW. and therefore the pt-ooer pacfung factor rn trhr lust CaICUlatlOn.
5. NOW thal CJkulattd
I
3.17
c’iotal
Ibs./sec.
JS aetemvn~
tt.mc.
c Ibs./tq.
of the to total
bed requfred mass transfer
from
of the torcr rhl~h; ana oDerated at the seecua Dressure
Step
4.
when oeragn amp
)(r;J
-ill
I
N
=
t-i A I’ A YLM because the drive IS from Or if a sttipping operatton fer co-cffioent becomes: Kra
the gas to me hqurd phase. 8s mvolvea then me mars
=
tmnS.
N
HAAXU
because the Qnve IS imm the liaufd to the gaS phase. The defin8bons of me terms for the r0ovc cquatfons for X.4 and Kra are as follows: Kd = Mass transfer CD-•ffioent lb. mola/ft.S Hr. Atm. = Mass tmnsfer co4fioent lb. moru/ft.J Mr. k. N = Lb. rnolc~ tnnsferred/Hr. H = Packed depth of tower paclung. ft. A = Tolm truss suxronal area. ft.2 P = System pmure. atmospheres Y, = Gas phase mole fracbon. component I Ye’ = Gas phase mole tractton of component i rn ecyutlibnum rnth kqutd bulk phase mole fractfon of ccfmpanent i. XI X, = Liquid phase mole fnctton, cOmPonent I phase mole fnctton of component I rn X,’ = Liquid equilibrium rcth gas bulk phase mole fnctlon of camponent i. Y, For cwnterturrent
gas-liquid
flow
determined
y-
I !
Page No :
be deoenoent “00” the, reaurreo with 1OOy mass, rncow8uiiy nqumng a bea of rnfmrte deptn.8 Therefore tow-a0 are ahays desqned to 00erate at I~SS. than total mass transfer. In gas J0~0rpt10n Dmbkms. the, bed is usually alculated from the mass transfer CD-. effioenti
the value of X as me abscfssa fn Step 1. and selected an aperatmg pressore drop m Step 2. the value of the ordmate. Y. may be determuwd by the use of the genmlrxed pressure dmo cornWon. Locate the value of me l bsassa on thrs chart: move vertralfy untff the pmper pressure drop prrameter 8s contacted: then move honxontalfy fmm thts pomc to the left hand edge of the chart and read the value of me ordmate. Make the value 4ual to thus group of vanaWe:
1. Then
0
equation:
6. The Qepth l ppmach transfer
should keep in mmd that the pressure dmo parameters shown on the generalized pressure am0 carrdauon are m Inches of rater (mm of water). Therefore. when oargnmg columns operatrng mth other lioutds. SW oal consldentron should be grnn. apeaally *men the specific gnnty of the liquid is substantially ICSS than that of water. For example. an rbsoorbcr handhng a hyOrour0On wrth a specffic gravrty of 0.5 wtll uhtbrt the propen~es of a t0wer rrth a hold-up volume corresponding to a pmsure drop l poroxrmatefy 80% greater man that for whfch It uas dacgne4. havmg
: z/es
establishes the dlrmeter wth the -clung sekcted kqudana gas rates. rnll develoo
qualiiy. The ducgner
. After
Date
Thcs filled
1.0 men of water prawn dmp per foot of packed depth (83 mm of water pressure drop 0er meter of packed depth). Htgher pressure drops are poiuble wfren mstfumentatfon IS such as to matntmn a constant prarun amp. Most ab sorben and regenerators are bes~gned for lw pressure drop ooeratron. l.c.. somewhere ktwcen 020 and 0.60 inches of water prcuure dmp per foot of packed depth (17 and 50 mm of water pressure drop per meter of packed depth). Atmospheric or pressure disMaUons art dcugnd for prurun dmps of 0.50 to 1.0 mcha of water pressure amp per foot of pcked depth (42 mm to 63 mm of water pressure amp per meter of packed depth). Vacuum dlStillabons run the complete nnge of pressure drop and aredependent on what is t0 De accomphshed and whether me va&um is solefy for impmved seoantlon or whether It ts to reduce tempenture of repantron to trnorove pdua
.
the
WhcrcAZ
the value of X consult the gcnerahred pesurc drop correlation l oove. It knfl be noteo mat there are a series of marked parameters rangmg from 0.05 to 1.5 jnchcs of water pressure drop per foot of Pachcd death (4 to 125 mm of rater pressure amp per meter of packed dCDth). Normally. a packed twer should be deslgoed to 00emte at J mammum economrcal pressure Omp. The du:gn l ngtner must determme the but balance between hagher apical uwestment vs. lower ooentmg costs for low pmsure drop twen. and low apttrl mvestment vl. hrgher
opentmg cysts amp. Ordinanlyy.
:
T-95
1 TEP/DP/EXP/SUR
1. To design tha JmOUnt determme bath liauid
Revision
ail vanaCMes have and the tyaamecer
assigned
of
the
values. G may tower aetermlneo
be Oy
AyLy
=
’
(YieY;‘)2-(Yi-Y,‘)1
La [
(Vi
‘Yi32
/ (vu *Yi’)l
1
where the subscripts 1 and. 2 refer to the top and bottom of the cOfumn rapectrvely. The equatfon of AX” IS l nafogouS to the equation for AYL. gfven above. La and Kra data are l vadable for most l bsorptron ana stnppng ooentmnr. 8eausa the data on absorption of CO, wth caustic soda solutfon are So complete for me various packmgs. it is not at all unusual to use the data as a ntto mformahon source for aesrgn wrth other packmgs and other rites than those for whrch dwrct rnformatron l xrst.s. Distillrtton umts are generally desrgnea an the basts of HEW (hcrght equrvalent to a thcoretfal plate).’ Hundreds of 01st1b Won l xDenmental studfa have caused US to conclude mat the pmpMws of a system have little to do wth the HETP value. pmviOtd that good dfstnbutfon IS marntarncd and the packed bed IS operated wth pressure amPs of at kast 0.20 mches of water pressure drop per foot of packed depth (17 mm of water prasure drop per meter of oackecl depth). Mass tnnlfer taking place rn packed beds. where any ~uO~tant~al amount Of pressure drop exrstS. wfll occur predommatcty IS a result of turbulent contact of gas and IWJI~ nther than as a offfustonal operatfon governed by film resistances at the mterlace. Once the total bed depth has been detcrmlned. the death of rnd~~dual beUs must be estabhshed. Gcneralty. ~nd~~dual bed defxh 1s held to l tght column etameters or 20 ft.. l nhougn under CeRam conditions 30 ft. Oeos are Mnnrssrblc. Prooer to-3 mternals are re~uwed to real~re me full poccnbal of the pachmg rn any l pphcatron. (See cng8nnrrng manual TAbOR.)
I
, PROCESS ENGINEERING DESIGN MANUAL
Revision
I Date
TEP/DP/EXP/SUR
il,
HEAT
EXCHANGERS
: : Z/85
Page No :
TOTAL
PROCESS
ENGINEERtNG
SHELL
TEP/DPIEXP/SUR
OESlGN
AND TUBE
MANUAL
Revision
EXCHANGERS
:
o
Page No :
Tf
Date
.: yss
4.1
1. APPLICABILITY It is not expected engineer.
For
calculation A quick
that a hand calculation
the
would estimation
A detailed
mechanical
single
of fluids
sheil
of the procedure
inside
or multi-pass
study
HTRI
diameter
any
required
by the rigo,rou!
or HTFS.
and tube
is given
in Section
length
should
be done by
3.
the scope of this guide.
on either
Exchangers
-
Reboilers
-
Evaporators
-
Fouling
-
Sea water
b. Shell
side :
1 shows the types of tubu,,.
;
found :
or forced
OR TUBE
highest
or corrosive
-
Condensers
-
Chillers
circulation)
SIDE
(using
refrigerants)
water,
steam
FOR THE FLUIDS
pressure
-
fluid
-
Fluid
-
Evaporation
-
Most of time
with the highest
Standard
length
.
Diameter
.
Pitch
commonly
with
squarepitch
-
used : 3/4”, used : triangular
on tube side)
Condensation fouling
fluid
fluid
: 12’, 16’, 20’ but longer
commonly
the sea water
- Least
in chiller)
lowest pressure
.
to install
viscosity
(refrigerants
OF TUBES
Cooling
fluid
(it is always recommanded
SELECTION
.
and can be
side : &Most of time
.
to requirements
Figure
standards
(Kettle) OF SHELL
according
side.
(Heaters)
-
TUBE
to TEMA
(Thermosyphon
SELECTION
varies
tube or shell
types are frequently
-
a. Tube
the exchanger
manufactured
The following
2.4.
area,
programs
be performed
NOTES
heat exchanger
2.3.
pre-project
exchangers
DESCRIPTION The flow
2.2.
or
using computer
design is beyond
AND
and tube
a feasibility
of heat exchange An example
DESCRIPTION 2.1.
of
be performed
hand calculation.
2,
purpose
of shell
tube lengths
are possible
(upto 40’)
I” External
or square.
tube
cleaning
is possible
only.
SIDE VELOCITIES
The
tube. side velocity
about
1.3 to 2.5 m/s.
Below
I to 1.2 m/s
become
a problem.
for .
most
fouling
will
materials
and services
be excessive,
much
should
above
be held between
2.3 m/s erosior.
can
-
PROCESS
ENGlNEERfNG
DESIGN
I
MANUAL
jge No SHELL
AND TUBE
EXCHANGERS
TEP/DP/EXP/SUR CHARACTERISTICS
2.5.
’
rigqrol
I I (
I ’ I THI;C$..lESS f BWC, 1 I
External diameter in et mm)
I I I
14 1 16 I 18 I
2.10 1.65 1.24
I 1
10 I :t j
I
16 I
3.40 2.77 2.10 1.65 1.24
1 1 in I (25.4 mm)
I I I I
!
I
I8 I 10 I 12 I 14 I 16 I
i
I
f
I
tubui,
I
I
I.
11/4 in
I (31.75 mm)
l8 I 10 1 it
I
!
I
I
I
I
16 18
I
I 10 1 :t
1 1
ll/tin 1 (38.1 mm)
de)
2.7.
2.8.
0.848 0.940 1.021
I f
4.2
GAGE (m2/m)
i WEICh
i External
1 Internal
f (kg’m
I I
I I
0.0266 0.0295 0.0321
I 0.6OC I 0.49C I 0.384
0.0384 0.0424 0.0466 0.0495 0.0520
I 1.436 I 1.216 I 0.96: 0.774 0.597
0.0798
0.0584 0.0624 0.0665 0.0694 0.0720
2.024 1.696 1.324 1.057 0.811
0.0997
0.0783 0.0822 0.862 0.0894 0.0918
2.604 2.158 1.682 1.34c I 1.024
0.0981 0.1021 0.1061 0.1093 0.1171
f 3.18’ I 2.63; I 2.035 I 1.62: I 1.237
1 SECTION
!
1
(cm2)
1 I
0.565 0.694 0.819
I
I
i I I I
I I 1
1.177 1.434 1.727 1.948 2.154
I
2-2v1 2.494 2.616 2.743 2.845 2.921
I I
I I 1
3.40 2.77 2.10 1.65 1.24
!
I
1.859 1.986 2.118 2.210
I
3.40 2.77 2.10 1.65 1.24
I
1.224 1.351 1.483 1.575 1.656
I I
;
3.124 3.251 3.378 3.480 3.556
I
I I I
.
minimum
temperature
.
minimum
pinch for condenser
DESIGN
AREA
0.0399
I
I
tI
I
1
)
4.885 5.375 5.909 6.357 6.701
I
1
7.665 8.300 8.962 9.512 9.931
I I
I
1I 1 1
I
2.714 3.098 3.523 3,836 4.122
I
0.0598
f I
1 1 I
I 0.1197
I
1 I I
I 1
!
I
5 “C. or chiller
3 “C.
10 % on area is recommended. DROP
.
Allowable
.
Liquid
Some
n P varies pressure
equivalent .
approach
MARGIN
PRESSURE
berween
drops
with the total of
gas drop is about
exchangers
have
than 0.1 bar) especially -
: 2f85
TEMPERATUREAPPROACHANDPINCH
.
possible
1 I
3.40 2.77 2.10 1.65 1.24
I 16 I I 18 I 2.6.
Date
Page No :
*
I (19%‘: Zrn) I 1 can b
WIRE
Internal ;, diameter km) I
done b l/2 in I (12.7 mm)
:
OF TUBES BWG = BIRMINGHAM
ZI by tt-
0I
Revision
0.7
to
system 1.0
bar
pressure per
and the phase of fluid.
exchanger
are
common.
Th
and condenser
(les
0.2 to 0.5 bar.
low pressure those in vacuum
losses
and as reboiler
system.
TOTAL
PROCESS
SHELL
TEP/DP/EXP/SUR
2.9.
ENGINEERING
AND TUBE
CHOICE
OF HEAT
a.
end stationary
Front .
DESIGN
MANUAL
Revision
EXCHANGERS
EXCHANGER
TYPE
:
Date
(Figure
o
Page No :
: 2/85
4.3
1)
head types
Type A : Used for frequent
tube
side cleaning
due to the ease of dismantling
the cover. .
Type B :
.
Cheaper
than
difficult.
To be used for clean
Type C : Cheaper
Type
than
Type
with the pressure. .
Type D : Special
A but
the
dismantling
b. Shell
types
.
Type E :
In general
.
Type F :
. Advantage
: Fluids
. Disadvantage
: -
The
type is practically
for high pressure
quick11
increases
never used.
used.
flow at perfect
leakage
counter
between
-decreases
current
the longitudial
(F = I). baffle
and shel.
in value.
-
mechanical
-
low
problems
pressure
drop
a great
number
from
expansion.
eg : < 1 bar (risk of damage
of the longitudinal
baffle). of Type E shells in series.
reboiler. Type G & H : Used for low AP = 50 mbar as for thermosyphon Vertical baffles are not installed for these types and due to thal
.
the length .
Type J :
of the shell
Used for high condensates
flow
Rear .
must
or high
be limited.
AP
for Type
to avoid the use of vapor
Type K : Used for vapor separation
. c.
price
P > 200 bar.
the most commonly
This type will be used only to avoid
is morf
products.
A for low pressure. This
of the bonnet
is required
E and also sometimes
or
belt. ie chiller,
some reboilers...
end, head types L, M and N : Fixed
Types low
AT
tube sheet,
< 30 “C. If A T > 30 ‘C
used for clean
use other
joint
cn the shell.
Type
L and N will be used for dirty
fluid
head
fluid
types
on shell side and fol
or install
an expansior
on tube side. For the other
cases the
type M will be used it is the cheapest. .
Type P :
Generally
not used.
.
Type 5:
Used very frequently,
.
Type T :
For frequent
dismantling,
5 for same number
d.
no restrictions.
.
Type
U : For clean
fluids
.
Type
‘7.’ : Generally
not used.
expensive,
of tubes generally
on tubeside
no other
shell
diameter
larger
than typt
not used. resrrictions,
low cost.
Conclusion The most
frequently
used types are : BES, BEW, AES, BEM,
divided
flow,
BEU.
PROCESS
-
ENGINEERING
SHEU
Page No :
DESIGN
AND TUBE
MANUAL
Rdvision :
I
EXCHANGERS
Date
TEP/DP/EXP/SUR w ~~~~ ,.xchonger
nommtclatura
FIGURE
1
imantlint
is more
E
s quick11 A
ONE
F
PUS
MU
w-----i WITM
TWO PAS 1OtGllUMNU
WELL
Mffl.E
IL and shell
B
G
sONNO
IINWL
COVER1
’ damage
D--,----,-
H
ies. C
-.
DoualESNl
e to thal CHANNEL INTKiML SlitIT AND RWVA8lt
times
WlTti
TUI COVtl
on
/I
J
FlOw
, _
MVIDED
flOW
rs... N e and for expansion
cases
-k .+
1 -
K
C+t*NNEL tNTCCPA1 wITI4 TUf WFn AND PEMOVAIlE COVE
-
the D
I SPKIAL
than
BEU.
type
-
WCti
mESURE
CLOSL
1
aoss
FLOW
-.
~-Page-Nay-r
0
I : 2/85
I
\ 4.4.
ITEM :
1 Q (2) 1 kcal/hr
DUTY HOT FLUID Inlet temperature Outlet temperature
T1 T2
COLD FLUID Inlet temperature Outlet temperature
t1 t2
Tl
I I
1
VALUE 0.5
1 I I t I
s
IC
NOTES G
fI Indicate
i i
:
temperatures’
@>b “-3
“C ‘C
I
“C “C
1 I rS I 26
- t2
T2 - tl LMTD
(1)
t2 - tl Ti - rl Tl-T2
I I
.
p - t2- tl Ti-tl
I i I
R=Tl-T2 t2 - tl
i I
F = LMTD factor
correction (2)
I
Number
of shell passes (3)
Number
of tube passes
HEAT
TRANSFER
HEAT A=2
TRANSFER
Fig. 2
I
Fig. 2
I,
k I
COEFF.
U 1 kcal/hr I m2 ‘C
AREA
I I
1; I
U.F.LMTD
I I -
m2
ESTIMATED ESTIMATED ESTIMATED
TUBE LENGTH SHELL DIAM WEIGHT l
1
I
I
I
‘Sfq’ u +a* p’dh I , id f3.4 - i cso t-k5
1
:c
( -0,)
I 2.76 I I 5. IS 1 s
Bundle\ tonnes Shell I tonnes Total 1 tonnes
PROCESS
II EZCA*o~Cf- Yw? I ficr, I .
IY
I
CALCULATION
t I I I I I
SHEET
ITEM: 6cz pL‘sc;c-;
TUTAL EPl~mlP/
I
I I I
-I I lr=o*q5
C?S
I i
I FT ins
I
including fouling factor
I
I
1
I
I
4oo
I
i
EXPlSUA
CM% I
TUE3E HUT
SHELL AND DATE
14lU
\
JOB
TITLE
:
EXCHANGER Fr3
Cih4cA~
NO JOE
:
E: ~23C N=
.
E y.\.wL:
REV
/I
TOTAL r,
PROCESS ENGINEERING
DESlGN MANUAL
AND TUBE EXCHANGERS
SHELL
TEP/DP/EXP/SUR
(I) Use following
formula
L,MTJ-J = (T2 - ti) - (Ti - t2) Ln T2 - tl Tl-t2
ifT2-tl>Tl-t2
LMTD
if Tl-
= (Tl
Remark
- t2) - (T2 - tl) Ln Tl - t2 T2 - tl
: If the heat by step partial
(2) For total
In this
with
are not linear
the LMTD
of the
and
linearisation
by the panial
duty
the
heat
correction
factor
of shell
and tubes
If F < 0.8 add shells Section
5 shell
transfer
the
determine
heat the
(Figures
on each linear
area
for each
with
be determined
the
ponderation
step of
the
step.
zone,
the T*irn of these
areas
is the
and tube
transfer number
.
2)
passes should
(2 exchangers
OF SHELL
ESTIMATION
be chosen
maximum
shell
in order
to have
1 < F < 0.8
in series)
heat
transfer.
DIAMETER area,
selected
of tubes
and
tubes with
tabje
diameter. Take
curves
should
for the exchanger.
the number
With
curves
condensing
(3) See LMTD
4.
the
LMTD
case calculate
surface
(4)-See
exchange
t2 > TZ - tl
diameter
about
60 inches.
size,
pitch,
tubes
length
1 or 2 hereafter
the
it
is possible
approximate
to shell
TOTAL
PROCESS
ENGINEERING
DESIGN
MANUAL
&vision
:
Cl
Date
: 2/8S
Page No :
TC
S-dELL AND TUBE EXCIihN~ TEP/DP/EXP/SUA FTc;uRE
I
4.7
TEPK
2
z ; 2 c0 _ = Y :0 I C
3 L ,:
LMfD
correction
factor
_.
TOTAL TEP/DP/EXP/SUR
PROCESS
ENGINEERING
SHELL
AND TUBE
DESIGN =mmNGERs
MANUAL
0
R&riotl
:
Date
: 2/8S
Page No :
4.8
roTAL
PROCESS
ENGINEERING
SHELL
EP/DP/EXP/SUR
SHELL
PITCJI NUMBER
0
TUBE
MANUAL
AND TUBE EXCHANGERS
I’
OF PASSE5
DESIGN
SIDE
I I
-
;
NUMBER
PITCH OF
A
I
:
0
Dhte
: 2/85
Page NO
4.9
I I
I’
PASSES
Revision
TUBE
SIDE
gH1
! API
I
8.
32
26
20
36
32
21
IG
32
32
40
60
>6
67
inc
I2
82
76
61
90
12
76
*-
13 I/b
9)
90
12
I09
IO4
90
IJ II4
137
124
II6
164
JJO
137
17 l/4
IAS
I66
15:
211
200
113
19 l/4
236
220
204
274
2%
211
21 114
276
270
246
320
306
279
23 114
323
31:
30:
3x3
375
3JO
23
107
39r
370
b7I
r>t
bl9
27
IO
460
632
29
SJI
324
480
31
633
616
169
33
7&O
712
615
3s
t23
a12
770
967
937
812
37
921
901
110
1074
I047
1014 1129
JM -
s3u
*a7
603
JS6
765
726
677
1JJ
130
772
630
_
39
I021
IOlk
913
1206
1173
42
1202
II61
II47
lb06
J3lJ
1310
45
1435
IYI I
1367
1639
I61 I
I%3
Cl
I62G
1398
lJ>J
1172
It4J
1766
>I
I911
1190
1148
2212
2113
2092
>6
221 I
2214
2167
2J68
254)
2446
2387
2356
2JlO
2987
294J
2127
60
T SHELL Bi in incMs
TUBES
i t I
PITCH NUMBER
bF
0 PASSES
TUBE
I
SIDE
f 4
PJTCJI NUMBEF.
I,
I
A
OF PASSES 2
1’
TUBE
c
I6
I6
20
I6
I6
30
30
26
37
30
26
12
b?
bJ
bl
57
51
47
33
II
67
61
57
a;
12
76
96
92
16
17 l/4
113
101
102
129
127
I17
19 II4
lb1
139
I37
170
160
JJO
199
II9
I79
21 l/b
170
I66
IJI
23 I/C
207
197
I97
246
232
215
25
248
2b6
222
294
281
257
2X7
287
267
349
s35
302
29
349
339
320
396
376
539
31
190
390
36)
472
4>6
431
432
bJl
J31
J20
467
610
192
J61
27
13
CJa
35
326
313
40
J7
J77
337
5s5
674
664
631
39
643
637
611
766
735
698
c2
746
729
109
900
45
a94
175
8>3
1018
IO13
912
*a
1029
IOIG
975
I Ita
II61
109x
>2
I216
!I96
I It.7
lUO>
1375
1321
56
1420
lb00
1638
160)
I>49
60
1639
ICI5
IIP9
IX>1
1797
:
PER
SHELL
I
SIDE
20
IJ 111
NUMBER
.
J/4
&
61
TUBES
1
I
IO
11 Ilk
MAXIMUM
1’
-i-
I’ II4
TABLE
7 -I
TABLE
WAXIMUY
lW8U
2
NUUBER
PER
SHELL
:a:
TOTAL
PROCESS
ENGINEERING
SELL
TEP/DP/EXP/SUR
DESIGN
MANUAL
Revision
:
0
Date
: 2/8S
Page No :
AND TUBE EXCHANGERS 4,IO
-
,- ‘WELL
.
AND
TUBE
HEAT
OVERALL
TRANSFER
waler/gas
I - 3s brr
170
vartr/gas
3s - 70 bars
230
- 39c
vattrlgas
70 - 100
bars
390
- xc
x am/gas
over
bars
JO0- - 700 340 - 440
100
Vattrlnrtural
gwlrnt
630
VatcrIMEA
(including fouling & Hearlnl/cwlrng
ra1tr/air
factors)
vattrlvactr
mcl (< 35 bard
240
- 340
cd/gas
UQUI
270
- 360
CdC3
chiIlcr
290
- 440
70 bars)
Ii-C.
rUCOuty H.C
vartr/he~*y
= BTU&ft20F = W/InLOK
- 1 occ
culgrc
vrttr/amagc
x 0.2047 x 1.162
- 730
70 - 120
P4tcrlli(hl
kcal/hzmzoC
- 230
0.5
ILLC
< 0.5 cpo
CpO
< viscosity
rucosrty
< 1 cpo
290
- 73t
250
- 610
50 - 500
> I cpo
300
Oil/oil
- 450
20-200
Dowthtrmlgu
30-300 s40
- 1 100
2:,-2x, 5cc~mfligh:
H.C.
~tamlamrgc
I
VPcosrly H.C.
Sttun/htary
KC.
0-s
< 0.3 c&lo
rrrcosity
soo-
CPo
< riscorcty
< 1 CPO
700
H.CJwatcr
Vawrlzatmn
(reboilerr)
- Lb0
340
- 390
S~c4m/oil
340
- J40
CUOllN/WJlCf
320
- 630
Htrry
I90
- 370
440
- 900
360
- 720
440
- >90
orcrbtadvattr
H.C.lrarer
Hydrocarbon
Irghthtam
Hydrocarbens Vrth
Set
7.
frgurts
3 and
REFERENCLS
4.1.
TEMA
4.2.
KERN
4.3.
LUDII’IC
4.4.
CAMPBELL
4 3.
NCPSA
4.6.
PERRY
4.7.
HTRI
Program
4.8.
HTFS
Program
4.9.
OUICK January
hot
’
C4-Cllrwam oil
4 hercrlttr.
AND
USEFUL
(smaaras
VOLUME
marw.facrwerr
assouatron)
cdrtron
1
g
CALCULATION 1910
cxchangtr
3 second
VOLUME Chapter
LlTERATURE
of tub&r
OF
- 1 700
420
Fracuonata
c.
loo0 - )oc
30 - 300
> I Cpo
sltamlvattr Laghc
230
HEAT
EXCHANGER
vElCHT
Process
Engl-rmg
TOTAL
PROCESS
ENGINEERING SHELL
AND
DESIGN
TUBE
MANUAL
Revision
:
0
Date
: 2/85
Page NO :
EXCF??GERS
TEP/DP/EXP/SUR FIGURE
3
TYPE AES WEIGHT ESTIMATE
4.11
TOTAL
PROCESS
ENGINEERING SELLI
DESIGN
MANUAL
Revision
:
0
Date
: 2/85
Page No :
AND TUBE EXCHRNERS
TEP/DP/EXP/SUR
FIGURE
TYPE WEIGHT
4.12
4
I
t
BEU ESTIMATE &se
I
: 3l4”
BWG
14 PITCH
: I-0
TUBES
LENGTH
?-
Q f 2 c).. 3 fc -
I I I II
16’
TOTAL
PROCESS
ENGINEERING
DESIGN
Revision :
MANUAL
AIR COOLERS
TEP/DP/EXP/SUR
Date
O
Page No :
: Z/85
4.13 -
1. APPLICABILITY For both the feasibility and preproject study it would generally be required to state tb required duty of the air cooler, the overall dimensions and weight and an estimate E required fan power. A calculation
procedure
2. DESCRIPTIQN
sufficient
AND GUIDELINE
for a preliminary
estimate
is given in section 3.0.
NOTES
Water or Air Coolinq ? .
Air cooling offshore is sometimes prohibited This may require installation of the air equipment. Use dosed loop water cooling.
.
Air cooling is cheaper, simple and flexible nuisance of water treating
.
is eliminated
due to the modular layout of the platf I cooler too remote from the associate’
vjhen compared
to water cooling. The cost ant
if air coolers are used.
In warm climates air cooling will not be as effective as water which will produce i cooler product stream. Air cooling is approx 50-70 % as effective as water.
‘Forced on induced draft ? Forced draft pushes the air at low&t power requirement. Accessability costs lower. Possibility efficiency.
to motor
and driver
available
are better
temperature
on
with forced draft of hot air recirculating
Induced draft gives better 2ur distribution recirculating of hot air.
forced.
(highest
Structural
P
and
) hence
lowei
main-rain.
!
into suction of fan thereby reducing
due to lower inlet velocity
with less chance o:
Induced draft Foolers can be easily installed above piperacks or other equipment Protection is given by induced draft coolers from effects of rain, wind snow on finnec tubes. Important if fluid in tubes is sensitive to sudden temp change also freezing oj tubes can occur in cold climates or heavy snowfall.
I’ i 1
TOTAL
ENGINEERING
PROCESS SHELL
AND
TUBE
DESIGN MANUAL
Revision
:
0
Date
,;u85
Page No :
EXCHANGERS
TEP/DP/EXP/SUR
4.14
Finned .
.
tube
1” OD tubing
.
(see Table
is most
Extended
surface
Standard
tube
costly .
elements
than
common
area
from
0.5”
to 0.625”
fins.
Fin
spacing
bare area.
6 ft to 50 ft
7 to 11 pir
inch.
.
(2 m to 15 m).
Longer
tube
designs
are less
ones.
Bundle
depth
may
smaller
units.
Use 4 as first
Fin material
with
is 7 to 20 times
lengths
short
2)
vary
most
from
3 rows
to 30 rows
of tubes.
4 or 6 rows
is common
for
estimate.
commonly
AL. Adequate
upto
400 “C operating.
Use steel
for higher
temperatures. Fans and motors .
.
Fans are axial-flow
large
efficiency
--
95 %.
Fan D equal
to or slightly
to 6 blades.
Max fan diameter
Distance
.
.
between
Fans may
be electric,
width.
Normally
fan efficiency
65 %. Driver
2 fans preferred.
Fans have 4
O-4-0.5
0.4.
steam,
of fan diameter.
Ratio
of fan ring
area to bundle
hydraulic
or gasoline
driven.
Individual
driver
site
usually
to 50 hp, (40 kw), 380 V.
.
Face velocity
.
A 10 % change
Temperature
of air across a bundle in air flow rate
control
of process
variable
speed
motors
.
Variable
pitch
fans more
.
Louvers
can be manually
.
For
process
recirculation General
is 300-700
results
ft/min
in -35
(l-5-3.6
% change
ms-l).
in power
used.
control
For dose
Note
Use total
14’-16’.
fan + bundle
not be less than
.
low DP devices.
less than bundle
area must
limited
.
volume
fluids
approach
: Air coolers carefully.
temperature
auto-variable
pitch
fans,
top louvers
or
are required.
that
system
outlet
efficient
than louvers.
adjusted
for winter
freeze
ai
temperatures
to maintain
air temp
or gel
is necessary
temp
to ambienr
are noisy.
Keep
or mght
air is 20-25
fan speed
time
operation. above
entering
“C. Absolute
as low as possible
the
winter
the tube min
is lo-12
and consider
ambient
bundle. “C. relative
layout
a
w
TOTAL
PROCESS ENGINEERING
DESIGN
MANUAL
Revision
:
0
Page NO
aate
: Z/85
4.1
GPER/ Duiy Fluid i
AIR COOLERS TEP/DP/EXP/SUR
Fluid c Fluid i: 4.0 REFERENCES 4.1.
Air am overal
AND USEFUL LITERATURE
Air cooled hear exchangers
PERRY
%E @ased
pp 11.23 > 11.25
-
Air cooled heat exchangers
LUDWIG
4.3.
Air cooled heat exchangers
GPSA
4.4.
Aerial coolers
CAMPBELL
4.5.
Design of air coolers - A
R. BOWN Chem. Eng, Mar 27 1978, p
Procedure 4.6.
for estimation
Estimate air cooler size HP 41CV program
STEP
pp 177 z 193
4.2.
chapter
l.Oprll rows ?r), -L
9
pp 207-209
N. SHAIKH Chem. Eng, Dee 12 1983, p
.
f’ 4.Y =c 5./\tal 6. EXIT 7. Aver D rm 8. Bare 9. Bare 10. Tu 11. Tu ,’ 30 14. 14. 15. 16. 17.
To Nu Fa PO Es. 4.1
Notes :
OPERATING
CONDITIONS
DuiY
AND
NATURE
OF FLUID
i 2% 10‘ kcaI/hr
iQ=
Fluid inlet temperature
IT1
Fluid outlet temperature bi Fluid inlet pressure
= j
too-
IT2=
i
50
IP=
J
10
I
46
WQ
4 I
‘C i FLUID bar abs J
Tf = TI _ T2 =
‘C I INLET m2 ‘C J
Ti=
30 I kcaI/hr
iU=
H-b-~
‘C
I tl = I
1 Air ambiant temperature j! Overall heat transfer coeff. ‘(see Table # and/or attached i work sheet) iI (Based on bare tube area)
:
So
‘C lc
l-1 - tI = -$o
200 I
,
NOTES
STEP i
l.Optimum
of tube
number
I
? 3 =Ot
,
air/&
m
f’-T2/Tl-tl 4.Y =&
airjT1
5.arair ‘I
- tl
= Y x (Tl
6. Exit air temp
;
7. Average
(1
Arm
- tl)
=Atair + tl
t2
temp.
differential
,At;ir
. i 8. Bare tube surface /, 9. Bare
tube
10.
Tube
’ ‘.
11. I-
Tubes/row ‘3ooler
Lo.
Total
14.
Number
15.
Fan diameter
I 16.
A b&
area/row
I’
:’
.
IN=
I
%
I
(curve
N” 4,)
IR=
1
0.8
I
(curve
N” 4)
I
1 0*314
lY=
I o-35
I
(curve
N” 5)
IAtair i 26.5 I t2 = 1 54.5
‘C I
rows
Fa=AjN
length TR = Fa/Lx0.08 width
W=TRx0.0635
fan power
=Fax0.795
of fans
Power/fan
17. Estimated weight 4.88 (36.4X9.35 N)xWxL 1 Curve Process
Notes 1
I
numbers Design
1’ -IDop/Mp/ 3Y
I
‘C
I IA=
1 326
m2 :
I
I
IFa=
I
IL=
I 7.5
41
lTR=l I
w
I
F,; 1 3, 4, 5, 6, 7.5 or 9 m are common I
1 4.3
m I kW I
t
PF
1 16.2
]
M
1 I? 500
I
m2 j
68
I Fp I ‘)2*4
I
refer to Manual Chap.
I’
I
(1” OD tubing)
max. fan diam = 4.6 m
I M I
kW I (including
kg 1 I
m’otors)
4.
PROCESS
CALCULATION
SHEET
ITEM: AIR COOLER fExP/
CHK
‘C
I
I 1 tm = 1 30.6
MnlT
TOTAL mmll
-
I
I NF I 2 I FD I 3-S
Fp/NF
‘C
NO
ram DATE
JOB
TITLE
:
JOB
E YAMG-
: N*
:
REV
1
1. LIQUID
COOLING
LIQUID
VISCOSITY
AT Tl
+ T2
GLOBAL HEAT TRANSFER (Read curve no 1)
2.
MASS
COEFFICIENT
: U =
kcal/hr
m2 “C
COEFFICIENT
: U =
kcaI/hr
m2 “C
COEFFICIENT
: U =
kcal/hr
m2 ‘C
: MW =
GLOBAL HEAT TRANSFER (Read curve no 2) TOTAL
CONDENSATION
Tl-T2
=
“C
GLOBAL HEAT TRANSFER (Rest curve no 3) 4.
CP
GAS COOLING MOLECULAR
3.
=
PARTIAL 4.1.
CONDENSATION WITHOUT inlet
LIQUID
AT INLET
gas flowrate
=
kghr
outlet
gas flowrate
WC2
=
kg/h
outlet
liq flowrate
WL2
=
kg/hr
=
“C
Tl
-T2
GAS MOLECULAR
WEIGHT
AT Tl ,-
HEAT (Read
TRANSFER curve no 3)
COEFF.
UC
HEAT (Read
TRANSFER curve nO.2)
COEFF.
Ug
GLOBAL
u=
HEAT
refer
TRANSFER
to PDM
GLOBAL COEFF. Chptr.
=
=
HEAT : U
OATE
kcal/hr
m2 “C
kcal/hr
m2 “C
kcal/hr
m2 “C
kcal/hr
m2 “C
4.
AIR COOLERS I-EAT TRANSFER COEFFICIENT
EXP/ SJA CHI(
=
PROCESS
TOTAL
=
COEFF.
m-0
P/mIMP/ \ I
+ T2
WL2 x Uc = WG2 x ug WC1 WC1
SELECTED TRANSFER Curves
WGl
JO8
TITLE
CAiCULATlON
SHEET
ITEM : NO JO8
: N*
:
REV
4.2.
WITH inlet
LIQUID
AT INLET
liquid
outlet
flow
liquid
rate
flow
rate
LIQUID
MOLECULAR
LIQUID
SPECIFIC
WLl
=
kghr
WL2
=
kg/hr .
WEIGHT HEAT
AT Tl
AT Tl
+2T2 =
+2T2 CPI =
kcaI/kg
=
kcal/hr
WC1
=
kghr
WC2
=
kg/hr
QL=(,)xCPlx(Tl-12) inlet
gas flow rate.
outlet
gas flow rate
GAS MOLECULAR
WEIGHT
‘C
AT Tl
+ T2
=
;T2
CPg
=
kcaJ/kg
- =
kcal/hr
=
kcal/hr
=
cpg
=
kcal/hr
m2 “C
ug =
kcal/hr
m2 “C
UC =
kcal/hr
m2 “C
u
=
kcal/hr
m2 “C
u
=
kcal/hr
m2 “C
I
GAS SPECIFIC .
QG
HEAT
AT Tl
= (WC1 + WC2) xCPgx(Tl-TZ) 2
CONDENSATION
HEAT
Qc=Q-QL-QC LIQUID
VISCOSITY
AT Tl
LIQUID HEAT TRANSFER (Read curve no 2) GAS HEAT TRANSFER (Read curve no 2)
HEAT
+2T2
COEFF.
COEFF.
CONDENSATION HEAT COEFF. (Read curve no 3) GLOBAL
TRANSFER
+ ut
COEFF.
+ u3
(4
SELECTEDGLOBALHEAT TRANSFER COEFF.
I /
:
BREl
PROCESS
TOTAL
EPmcPfDlP/ EXP/ SUCI 1 CHK I
U
TRANSFER
u= *
WT DATE
“C
AIR COOLERS TRANSFER COEFFICIENT JOB
TITLE
:
CALCULATION
SHEET
ITEM : NO Jot3
: N’
:
REV
c
PROCESS
ENGINEERING AIR
‘DP/EXP/SUR cF.vE
1
-COOLING
DESJGN
MANUAL
COOLERS
HYOROCAA8ON
Revision
:
0
Date
: 2/85
Page No :
4,2Q
LIOUIOS
I
HIGH AI? LOW
03
01
0.4 0.5 0.6 0.70.8
2
1
u CURVE 2
/
-
FOULING
FACTOR
3
4
Ln -cca1/hr.m2
-c
5
6
7
CASES
COOLING
I
I
I
I
I
I
I I
I
2
3
4
5
6
78910
20
30
I
I t
PRESSURE 1
8910
L
BAR 1
40
50
i
i
ASS. ,I60
70
-~
TOTAL
PROCESS
ENGINEERING AIR
DESIGN
MANUAL
0
Revision
:
Date
: 2(85
Page
NO
COOL==
TEP/DP/EXP/SUR
4.21
I
800 700 600 500
200
IS0 /
PRESSURE
2
1
3
4
5
10
BTLJ/hzft20F
*
x
4.885
20
F.m h..,)lt
data
CI Fins/inch
I
JO
40
50
in. h
l-in.
00
tubes
*
T+c*l
owrdl
3.00
S.SB
AU.
sq +t/if
IA.5
21.4
Tube
Pitch (3 rows) (4
rows)
I
2 inA
I 70
1
kwu-drr k
$6 in. LT 10
ft/ft
APSF
rq
I
c.
TABLE .I.
e~F4urm
rrbm
-
APF,
ABS
BTu/hrft2”F-
for y,
I
I
= kcal/hm2
we=2 Fintube
BAR
2%
In
68.4
60.6
91.2
00
J
2%
In
09 0
A 1
I-‘“-
2%
10 80
118.8
107.2
(5
rows1
114.0
101.0
148.5
134.0
(6
rows)
136.8
121.2
178.2
160.8
3 4
,.-.-c-ebw--cJ-t~,-O.wll................. amcrr we (~,-awa.. sGY)--r ,,,.OWl,............... 30-m -se” (.,9o.wzl...............
C.
u,
k--t.
“.
Ub
II+?
I
.,-a
I
-1 h%J
1-t “O-L, 1-. 93-4
u.
:
TOTAL
PROCESS
ENGINEERING
/
AIR
DESIGN
Revision :
MANUAL
0
Page No :
COOLERS Date
TEP/DP/EXP/SUR
: 2/05
4.22
CURVE
4
0.4 02 a.2
500
Y=
I
I
0.1 600 OVERALL
HEAT
700 TRANSFER
800 (ban
CilJIr 11
.I1
0.7
0.C
0.5
0.4
.A
9
0.3
1
I
I
I
I
I
I
I
0.2
I
I
tutu)
TOTAL
PROCESS
ENGINEERING
PLATE
TEP/DP/EXP/SUA
DESfGN
TYPE
MANUAL
- .
EXCHANGERS
:
j I;;rnz2,,“,
,
pag;z’
1. APPLICABILITY
FEASIBILITY
STUDY
tinder
normal
vendor
based on process
Two types
circumstances,
of plate
exchangers
Plate
fin excfiangers
.
Plate
exchangers.
the purpose
the
of this
design
data supplied
.
For
.
: PRE-PROJECT of plate
type
exchangers
would
be aetailed
by a
by the engineer.
could
be used :
;
design
guide,
only
a quick
description
and some
characteristics
are
given. For plate For
fin exchangers,
plate
VICARB)
the size could
exchangers,
the
information
An estimation
of the
heat
known
using the same
factor
= 1. The heat transfer
DESCRIPTION
AND
2-l PLATE These
FIN
transfer
formula
be estimated
area
could
as for shell coefficient
C;uids,
pressure
be done
and tube
vendor
if the
heat
(ALFA-LAVAL,
to estimate
drop,
spacing,
plate
heat
exchanger
is difficult
APV,
transfer with
coefficient
a LhZTD
; it depends
is
correction
on many
factors
ect...
EXCHANGERS
frame
consist with
of stacked
openings
corrugated
for the inlet
liquid
salt bath to braze
all the separate
Flow
in adjacent
passages
several
if some
NOTE5
exchangers
an outer
could
only by a vendor.
are available.
as flow rate of different
2.
size
be done
fluids
fluid
can be exchanging fluid
can heat
is a two
sheets
and outlet parts
at the same
inlet
phases
phases in order
to have a good distribution. \;a -only
flow
of fluids.
This
counter
current,
by flat
plates
core is immersed
and in a
or crossflow
and
time. a drum
aPi d-w---with
separated
together.
be cocurrent,
In case of the
(fins)
clean
is required ycq+alrc’
fluids.
to separate FL””
the
two
b c4-.hw
OTAL
PROCESS.
ENGINEERING
DESIGN
MANUAL
Figure
1 shows the principle
surface
can be accomodated
IMaximum
design
Temperature
of construction in a small
pressure
range
Size max. Temperature
approach
Applicability Pressure
drop as for shell
clearance
of a platefin
volume
between
54 barg (some
:
- 195 “C to + 65 “C
:
1,220
:
2 “C
:
LNG,
is easily
The
can be made
corrosion
floor
The
two
to figure
and small
and are used a small
of metal
A large
amount
of
models
claim
80 barg)
x 1 340 mm
from for
temperature
temperhture
:
250 ‘C’
transfer
through
heat
transfer
can be used.
such as titanium They
overall
are
very
which
are resistant
compact
exchangers
to and
coefficient
Water/water
:
2 000 - 5 000 Kcal/hr
Maximum
surface
:
about
Maximum
flow
:
2 500 m3/hr
Applicability
: Sea water
.
drops
Pressure
- service
: allowable
and the service
water-TEC
REFERENCEAND information.
m2 “C
1 500 m2
water, pressure
water-TEG, drops
TEG-TEC, vary
according
.-. to
the
tocal
system
of the fluids.
- service . coefficient),
sea water
transfer for
each
gaskets)
heat
for
a small
area.
Maximum
pressure
to give
directions
A good
differences
coolers.
10 - 20 bars
special
if required.
materials
sea water
by gaskets
pass in opposite
for deaning
exotic
separated
2.
:
Vendors
exchanger.
4.24
...
plates
fluids
pressure
-
recent
recovery,
Maximum
-
,usi
heat exchangers.
dismantled
is obtained
plates
plate.
Refer
coefficient
Overall
Date
Page No :
mZ/m3).
mm x 6 096 mm
LPG
and tube
each
plate.
The exchanger
(Need
(1,000
:
are an assembly
alternate
occupy
O
EXCHANGERS
Plate exchangers every
:
PLATETYPEEXCHANGERS
-“/DP/EXP/SUf?
2.2 PLATE
Revision
water
or TEG-TEC
: 0.5 to 2 bar (high
the dP could
USEFULLITERATURE
be very
A P increase low such
the overall
as 10 to 20 mbar.
heat
TOTAL
PROCESS
ENGlNEERlNG pm’r~
DESIGN
FIGURE 1
Revision
:
0
Date
: 2/85
Page No :
EXCHANGERS
TEP/DP/EXP/SUR PLATE
MANUAL
FIN ESCSA!!GZfTS
4.25
TOTAL
PROCESS
ENGINEERING PIATE
TEP/DP/EXP/SUR
DESIGN ExctIANGuzs
MANUAL
Revision
:
0
Date
: 2/85
Page No :
DETAILS OF PLATE TYPE EXCHANGER
IWO5
II
10
loo-165
3605
11 --
!O
160-265
1,;
3605
11
10
260-340
13
.i
x05
11
IO
33sao
21
2
3960
13
0
roe-700 .-
1
2940
9 7)
2525
s
:
3515
19 6i
3100
10
3
4055
13 lj
IWO
11
1
AJ65
I.
4070
5
6660
22
6AAS
Ii 2 --
6i 6
.
.-
4,26
. r
TOTAL
PROCESS
ENGINEEA!NG
DESIGN
MANUAL
Revisidn
:
0
Date
: 2/85
Page NO :
FURNACES
TEP/DP/EXP/SUR
4.27
1. APPLICABILITY It is not
expected
normally
done by a manufacturer
Furnaces
are used to transfer
duty 2.
and produce
that
high
a hand
calculation based
heat
process
of furnaces on process
directly
data
to the
be performed
supplied
process
by the engineer.
it is
by the engineer.
fluid
and generally
have a large
temperatures-
DESCRIPTION 2.1.
A furnace
consists
.
A combustion
chamber
.
Tubes
are
which
transferred .
2.2.
of the following lined
fluid
are located
externals
which
is also lined
with
.
Stack
for disposal
of flare
.
Air supply
.
Instruments
system
refractory
within
to the process
which
22.1.
with
located
Tubes
TYPES
:
the
and burners
combustion
chamber
and
where
heat
is
by radiation
to the combusion
chamber
in a convection
zone
refractory. gas.
by fan or induced
draft.
and controls.
OF FURNACE Cabin
.
furnace
This
is a rectangular
vertical.
The burners
zone is located .
.
gases discharge
draft
fan.
and contains
are situated
above
Flue
to a stack
are normally
arranged
provide
a radiation
zone
on the
in the floor The
or floor,
bank
is obliged
can be horizontal
or
and the convection
A small
negative
of
.
There
is a pressure
either
by use of a fan discharging
arrangement
tubes
by an induced
and are spaced
so as to
and
flame
avoid
is bxners
located
1. across
which
the
flue
gas
to pass.
is maintained
loss’ ilr the
stack.
or are driven
temperature
in Figure
rows
.
in a tall
constant
as shown
contains
pressure
directly
An alternative
the furnace
draft
which
in rows on two walls
leaving
creating
in the walls
either
of
tubes.
of the furnace
connection
tubes
the furnace.
Burners
impingement
.
furnace
flue
to prevent gas system
to a short
hot gas leakage. and this has to be made
stack
or by natural
bou).mcy
up
PROCESS
ENGINEERING
DESIGN
MANUAL
Revision
:
0
Date
SW35
Page No :
FURf’JACES 7P/DP/EXP/SUR 2.2-Z.
Cylindrical .
.
furnace
(see Figure
These
furnaces
are vertical
solely
a radiation
zone.
The
burners
vertical
are located
or helicoIdal.
zone and contains Generally
.
2.3.
Two
types
of burner
and forced 2.3.1.
draft
Induced
can
required that 2.3.2.
EXCESS
is located
zones
zone tubes above
or
can be
the radiation
tubes.
above
the convection
bank
with
no fan.
burn
above
gas or fuel
oil
air
or natural
The
for
air
oil of steam
pressure
is required
draft
burners
or independently.
for atomising.
Excess
air
liquids.
If fuel
oil is
(Excess
air indicates
ratio)
burners
and the burner
simultaneously
gas and 30 % to 40 % for
the stiochiometric burners
the
excess
burner
air system
From
this
is supplied
can operated
air
recommended
proposed.
See § 2.3.
determine
with
by fan.
It
less excess
is therefore
capable
of
air 5 to 15 %.
the
kg of
by the
flue
gas
per
burner
kg of
manufacturer
fuel
fired
and the
remembering
type
that
of
air
21 95 Vol of oxygen.
GAS TEMPERATURE
is controlled The
induced
burners.
Pressure
Determine
STACK
in furnaces,
AIR
contains
process
by 2 factors fluid
the convection .
is vertically
and convection
and the radiation bank
rows of horizontal
are used
0.3 kg/kg
control
.
in the bottom
is 15 % to 20 % for
burned
This
radiation
air burners
These
.
and contain
BURNERS .
.
1)
The convection
the stack
4.28
Condensation
inlet
:
temperature
will
determine
the
temperature
is present
in the fuel
of the gas leaving
bank. is to be avoider.
raised
to avoid
the
result
in a minimum
possibility exit
if sulphur
of production
temperature
of about
of corrosive 120 “C.
the stack
sulphurous
temperature
acid.
This
is would
c
TOTAL 1
PROCESS
ENGINEERING
DESIGN
MANUAL
Revision
0
I
FURNACES
TEP/DP/EXP/SUR
Date
: 2/85
heat
in fuel and
4.29
5. EFFICIENCY 1
If
flue
Hc = Hf =
=
gas enthalpy
enthalpy being
Losses include
.
For a furnace
.
A furnace
6. PRESSURE
.
Convection
radiation
bank
IS galned
using natural
GASES
bank will be from
fuel (2 % is a good is of the order
figure).
of 50 to 55 96.
75 to 85 % efficient.
3 - 15 mm-water
.
Ducting
:
variable
:
5 - 15 mm water
.
Stack
:
variable
buoyancy draft
of hot stack
burners
gas.
a low pressure
loss is required
across the burner
and
pressure.
leave the stack at 10 - 20 m/s velocity
of 60 x lo6 Kcal/hr
as the maximum
diameter
A cabin
requires
furnace
requirement a cabin
as 27 m. will
safe dispersal.
to ensure
If the be
furnace
floor
gives
construction
problems
area than
a cylindrical
furnace
the length
can
are horizontal then a withdrawal space for tube However for offshore applications the space required. the cabin
15 m.
tin
furnace.
to obtain
a uniform
heat
release
across the radiation
.
it is not possible
zone. The height
furnace
tubes
It is possible
can be about
the cylindral
10 - 11 m.
much more
also
furnace
a cylindrical
the radiation
is about
tends not to favour
zone. The height With
heat
OF FURNACE
a capacity
replacement
.
+
VELOCXTY
OF TYPE
Above
With
duty the efficiency
under negative
operates
be as much
.
e.g. unburned
:
by natural
The flue gases should
.
is all radiant
air regulation
the furnace
.
air)
if required.
and unaccounted,
with a convection
For a system
8. CHOICE
steam
value + sensible
is lost in :
Burner
7. FLUE
(net calorific
LOSSES
.
Pressure
of combustion
which
t
at exit
by atomisation
.
Pressure
100 - 100 losses x Hf Hf - Hc
be about
to obtain 25 m.
a uniform
heat above release
across
OTAL
.PROCESS
ENGINEERING
DESIGN
MANUAL
Revision
:
Oate
: Z/85
0
Page No :
FURNACES TEP/DP/EXP/SUR
9.
ESTIMATION
OF SIZE OF CYLINDRICAL
The following
is for a very preliminary
D=
FURNACE sizing
G
D in m
Qa =
absorbed
heat
0
=
D+l
m
H
q
2.5 D
m util
in 106 Kcalfhr radiation
bank
,
COrrCCTlO* IOUC
i
TOTAL
PROCESS
ENGINEERING
DESIGN
MANUAL
TEP/DP/EXP/SUf?
.
I
. 1 I’
.5,
--_
PUMPS
Revision
:
Date
: m5
Page No :
TOTAL
PROCESS
ENGINEERING
DESIGN
MANUAL
Revision
:
0
Page No :
PUMPS
TEP/DP/EXP/SUR
Date. 2/85
5.1 I ’
I .O APPLICABILITY For
both
: Ii
the
feasibility
evaluate
a pump
In order
to provide
the type
study
selection
and
and fill
a pre-project
study
in a data sheet
with
the basis of a good cost and layout
and’ number
of pumps
for
the
service’
the
engineer
will
be required
to I
the basic information. estimate
it is important
in consideration,
to understand
and the associated
I
power
requirements.
.I
2.0OFtCRIPTlONANDGUfDELINENOTES TYPES
‘I
I
OF PUMPS I
.
Generally
there
are three
Centrifugal 1. Centrifugal 2. Propeller
3. Mixed 4.
’
flow
A pump
:
Rotary
Reciprocating
I.
1. Piston
Cam
2. Screw
2. Plunger
3. Gear
3.
Diaphram
4. Vane
Peripheral
5. Turbine .
classes of pumps
5. Lobe
selection
chart
GENERAL
USAGE
Centrifueal
pumps
.
kledium
to high capacity
.
Higher
head requirements
.
General
service
.
Simple,
low cost,
(Process
is shown in Figure
1.
I’ I
Pumps) for low to medium can be met
for all liquids,
by using
hydrocarbons,
even flow, small
floor
head requirements. multistage products,
space, quiet,
impellers. water,
boiler
feed.
easy maintainance.
I
I
I
I
OTAL
PROCESS
ENGINEERING
DESIGN
MANUAL
Revision
PUMPS
:
0
Page No :
I
1 TEP/DP/EXP/SUR Rotary
Dumps
.
Many
.
Essentially
proprietery
liquids
can handle
with dissolved
.
Can handle
.
Typical
.
available clean
for specific
fluids
only
gases or vapour
wide range of viscosities
fluids
pumped
molasses,
alcohol,
Generally
specialist
Reciprocating .
designs
: mineral,
mayonaise,
services.
with
small
suspended
solids
if any. Can pump
phase. - upto
500 000 SSU at high pressures.
vegetable,
animal
soap, vinegar
pumps for specific
oils, grease,
and tomato
glucose,
ketchup
viscose,
paints,
!
requirements.
pumps
Pumps
produce
pistons
and casings.
.
Overall
efficiency
.
Piston
pumps
intermittent
virtually
any discharge
is higher
than centrifugal
: can be single services.
head upto
or double
limit
pumps. acting.
of driver
Flexibility Used
for
Less expensive
than
plunger
pressure,
duty
or continuous
power
and strength
of
is limited. low
design
pressure
but
cannot
light
duty
handle
or
gritty
fluids. .
Plunger gritty
.
pumps
: high
or foreign
Diaphram
material.
pump
parts
Ideal
for toxic
slow speeds for delecate . I
Triplex
pumps
REFERENCES
USEFUL
4.1.
LUDWIG
4.2.
PERRY
4.3.
CAMPBELL
VOL II
4.4.
“Centrifugal
pumps
“Rapid
used for TEC
by plastic
material.
usage.
circulation.
HANDBOOK
CHAPTER and system
I. Karassik
Chem.
W. Blackwell
14.
Engrng
Ocr 4 1982
of a Pumping
Oil and Gas 3. Nov. of Centrifugal-pump Chem.
6
Hydraulics”
Speeds up Selection
calculation
3
CHAPTER
Eng. Janv.
unit”
12 1979
hydraulics” 28 1980
or rubber
Can be pneumatically
LITERATURE
ENC.
.M. Seaman 4.6.
fluid
CHAPTER
CHEM.
“New Program
from
or hazardous
VOL I
Ugor 4.5.
are sealed
fluids.
: commonly
AND
service
Suitable
for
diaphram.
No
Expensive.
: driven
seals no leakage.
heavy
driven
at
TOTAL
PROCESS
.
MANUAL
Revision
PUMPS
TEP/DP/EXP/SUR
1. FLUID
DESIGN
ENGINEERING
:
0
Page No :
Date z/S3
! i TEPfC
5.3
CHARACTERISTICS
Always
quote
at pumping
temperature
ie : normal
suction
T. 6. -F
2. SUCTION .
PRESSURE
Evaluate
at pump suction
Ps = Pop + Static Pop = minimum Static
flange
head - line loss vessel operating
head : evaluate
at LLL always
h2 (approx.
0.1 bar/100
.
.
available
always
try to provide
Vapour
correction
pumped
from point
-
static
head above pump
0.6 m). head (bar) = m x specific
centreline.
gravity/lo.197
7. -F
etc : for estimate
use
NPSHR
is stated
I\
m.
SUCTION
NPSH,
bubble
take
bara.
APline for bends, fittings,
Line loss : evaluate
3. NET POSITIVE
pressure
HEAD
NPSHA
is evaluated
by the ,engineer.
0.6 - 1 m NPSH is calculated
the calculated the vapour
than vendor
more
by substracting suction
pressure
pressure.
the
required states. vapour
Convert
by the vendor
this
pressure
of the fluid
to m head.
beil,G
For a fluid
at
= Pop
head (m) = bar x lO.l97/SG. INPSHA 4.
DISCHARGE .
Dellvery
.
Static
= static
head - line loss + vapour
PRESSURE pressure
- use maximum
head h3 - height
Pop of destination
of delivery
vessel the height .
A P discharge
line - calculate bar.
.
correction
a P exchangers,
heaters,
point
above
vessel pump
or if a submerged
discharge
into
a
9.
of the HLL.
based
on line
length,
fittings
etc or use minimum
of 0.5
’
A P from equipment etc - use allowable 0.7 - 1.0 bar if not available.
10.
data
sheets.
Estimate
!
PUMPS 1
TEP/DPI
EXP/SUR
P/85
Date
5.4
I‘! 1
.
A P orifices
.
A
.,
- for flow meters
P control
valves
use 0.2 - 0.4 bar.
- use maximum
valve
of 0.7 bar, or 20 % df dynamic
friction
losses
or 10 % of pumpAP. .
TOTAL
5. DIFFERENTIAL .
PRESSURE
DISCHARGE
- sum of aIl abovea
P values.
HEAD
Discharge
pressure
- suction
pressure
convert
to m head
6. FLOWRATE .
Normal
flowrate
is maximum
.
Design
flowrate
.
Design
margin
Use
10 % for feed pumps or transfer
is normal
20 % for reflux 7. POWER Note
metric
.
Brake-horsepower
.
Operating
8.
Note
.
horsepower
- theoretical
fluid
(BHP)
-
load - electrical
input
Shut off pressure
PUMP .
10.
.
MINIMUM
used power
requirements
are given
in kW for
HP = flow
HP/
p pump
to electric
driver
efficiency
Kw
power
to motor
at rated
x head/36
KW
efficiency
KW
at normal
motor
pump
operating
load
=
size Kw
1 450 rpm or 2 900 rpm
PRESSURE = max suction
(shut off pressure) pressure
(calculate
at HLL
and p
maxi)
pump AP
FLOW
For an estimate
PUMP
pumps
nm motor
load - electrical
DISCHARGE
hydraulic
+ 120 % x normal 9.
feed water
is still
pump speeds are either
MAXIMUM
margin.
pumps
“horsepower”
BHP/
.
+ design
flow
calculations.
Hydraulic
Connected
operating
’
the term
.
.
flowrate
pumps and boiler
REQUIREMENTS
: although
long term
use 30 % of normal
flow.
WEIGHTS
For an estimation centrifugal
pump
purpose package.
only
Figure
4 can be used to determine
the weights
of a
Indicate
FLUID
PUMPED
: Liquid
:
Pumping temperature T : Vapor pressure at T : Density at P, T Specific gravity at P, T i
SUCTION
NET
elevations
36 l-04
POSITIVE
s22 o-822
1 I DISCHARGE
SUCTION
t HEAD
\* ”
1 I I St!5 I l,a4
I
AVAILABLE
MAXIMUM
m
NPSH
SUCTION
,I TOT ’
: \( z$$s
baral bar I
net bara MAXIMUM
DISCHARGE
PRESSURE
suction pressure Normal pump AP x I20 % Max.
.
bara; 4.0 bar I I
net bara N&S:
:, S;uA cr
3.5 O- S
I
I
I
lo 000 as*93
cf’ m3/h % m3/h I I I i
i*ol I a29.y o*+ 0.30
.I
*I-
‘,
I
I
-
f
I
I I I I
0.4 0.5
1
I
bara
1 4.6
bara bara
t I ; .l*(e I 4.6
’
t I
PRESSURE
I I Suction Pressure I Discharge pressure I I PumpAP
bar m 8’ I.
.
‘I I POWER REQUIREMENTS 1 I Brake Horse-Power = I x 2
CALdJLATlON
SHEET
kW
42030
1 3.42
(2);
I43 I I
t I’
t I 322
I
I I i
,
3 I f
375
4 i
1 400
5 I
I
I I I I IS’too I
I
f I 51 I
’
ITEM : PSOWCl “0:
t i
I
I (Fig 2 for 377 I 1’ 5l.q; Estimated motor size kW I I Design operating load 4/fm kW I (Fig 3 for ?rn) I I I Estimated weight kg I PROCESS
I PUUP
PRESS
I DIFFERENTIAL
i-91
I 14.0 L
DISCHARGE
I i I I 1 I I
s ?.q-
I
I I
PRESSURE
bara bar bar bar bar bar bar bar
I.
-
I Vessel PSV setting Static head at HLL
PRESSURE
I 2 F line loss C&~-C> I Other
I
,i
3.2 0 .eoe 151 2-s 189
f
[ -03 I’ z[ Delivery pressure 345-G._ I Static head <-&I o-251 I AP control valve(s) 0.10 I AP exchanger(s) I AP orifice(s) I
PRESSURE
$.“i;&
: : :
bar al m 1 bar 1 bar!
m Static heado LLL .z :L :,. <.r/ m - Line loss + vapour pressure correction m TOTAL
sketch
Viscosity at P, T Specific gravity 15 4 Normal flow Q Design margin Design flow (1)
‘C bara kg/m3
PRESSURE
SUCTION
and system
PUMP TYPE : c~rqaiCu<*c 2z?oo rp Speed :
c9dM
, Min. Origin Pressure= Static head Q LLL = (m x sg x O-0981) - A P suction ,line ,- , PUMP
pressure,
PrtiP 4/O
i
IT
TOTAL
PROCESS
DESIGN MANUAL
ENGINEERING
Pegs No :
TEP.‘DP/EXP/SUR
Date
FIG.
I
SEWERAL
FIG. 2
4m
OF
APPLICATIOW
ESTIMATION
FOR
OIFFFREHT
OF CENTRIFUGAL
PUUP
PUMPS
TVPEL
: 2/8S
FLOW
(M’tn~
EFFICIENCY s
60 70 60
so 40
30 20
CAPACITY
rn3/ h
TOTAL
PROCESS
ENGINEERING
DESIGN
MANUAL
P!JtlpS
TEP/DP/EXP/SUR
FIGURE ELECTRIC
MOTORS.
Condiuoru -BHP 0.51 0.75 1.01
0
-
2.01
-
Il.01 6.01 1.01 12.1 16.1
-
0.3 0.75 1.00 2.00 b-00
-
20.1 26.2 3b.9 b3.6 52.3
-
26.1
-
w.1
-
b1.S j2.2 65.2
30 a0 SO 60 IS
65.1 17.1 113 137 IX3
-
17.0 114 136 112 227
LOO 125 IS0 200 250
-
273 )I: 364 co9 bSS )us
ma 1so
Applies 10 k
COO
bS0 SO0 600
to loftily enclosed aed in detcrmirution
GRy
WEIGHT
ESTIMATE
7s 10 II :t
-100
12 13 7: 79 13
82.5 71 LO 10 80
10
Xl.> X5 86-S
‘/I
tJ 86::
(1)
Power Fxtod21 % of FuU Lord CAOACIW
Motor Efficienq pi of Full Lord CW-rl EE lo
67 7s 75 81 T-112 IO 15 20 2S
(1)
& EFFICIENCY
a1
6.00 1.00 12.0 16.0 20.0
221 27b 319 365 610 656
Notes2
REC&4MENkl!3fE
Probible Motor Rating HP
AI DAgn
3
10 :a Ib
t6 16 90 91 91 90 90
88 86
90 91 91.5 90 19 19 19-J I% 91 92-S
91 91.J 91 92.5 93.5
91 92 92 92 a9
90.3
93
90
91 It 91.3 93
93 93 93
ii: 93 93-J
93 93
9b
9b.J
8b
13 86 11 90
motors only (i.e.. cxplorron of KVA’r if dcrtrd.
FOR CENTRIFUGAL
PUMP
i
t: 91 90
proof)
.
PACKAGE
HORSE
POWER
-
TOTAL
PROCESS
ENGINEERING
DESIGN
TEPIDP/EXP/SUR
7,
COMPRESSORS
MANUAL
Revision
:
Date
: 2f85
Page No :
TOTAL
PROCESS ENGINEERING
DESIGN MANUAL
Revision :
0
Page No : ’ TE
COMPRESSORS TEP/DP/EXP/SUR
Date
7.1
: 2/85
..’
-1. APPLICABILITY For
both
feasibility
compressor
selection,
To evaluate
method
AND
TYPES
reciprocating
.
rotary
GENERAL
it is more
required
to
evaluare
2
I
.
a data sheet.
accurate
to use SSI instead
of
here.
in consideration,
GUIDELINE
it is important
and the associated
to understand power
the
type
of
!
!
requirements.
NOTES
(volumetric)
selection
chart
compressors
Reciprocating
compressors
Instrument
.
Low capacity/high maintain
Rotary
.
axial
are :
1..
are widely
used in the oil and gas industry
and service
For example
:
air compressors
pressure
the gas lift
ratios.
for small
gas compression
for re-injection
of field
gas to
!
capability.
compressors types
industry
of rotary
compressors
are as follows
Lobe compressors
.
The reliability
.
tVRoots” type compressors Screw
frequently
type)
employed .
is generally
in the petroleum
higher
Screw compressors
than reciprocating
are used where
machines.
a high flow rate
’
with a relatively
is required.
compressors
insirument Centrifugal
(“ROOTS”
factor
low-pressure
most
:
.
.
centrifugal
gas flows and high compression
.
.
.
is shown in Figure
Reciprocating
The
industries
USE
to medium
2.2.3.
and power
(volumetric)
A compressor
2.2.2.
be
power and complete
types used in the oil and gas processing
.
2.2.1.
temperature,
will
engineer
OF COMPRESSORS
The principal
2.2.
the
the basis of cost and layout
for the service
2- DESCRIPTIOil
studies
temperature
presented
to estimate
compressors
2.1.
discharge
the discharge
the manual In order
and pre-project
are
and service
sometimes
used
air for installations
in low of small
flow
gas service
to medium
or for
size.
0
/
compressors
These
Centrifugal
power
per unit
are less than
compressors weight
and essentially
rf:iprocating
costs may be hi;
have
-.r. Frequently
become
popular
vibration-free.
compressors used
very
in the
but efficiency oil
Initial
offering
more
costs normally
I
is less and utility
ar.d gas process
industry.
,
6.
I r
w\y c-
0:
TOTAL 1
I
PROCESS
ENGINEERING
DESIGN
I
MANUAL
1
.j
2.2.4.
e
2
:
0
Date
: 2l85
Page No :
COMPRESSORS
TEP/DP/EXP/SUR
-.
Revision
73 L
Axial
compressors
These
machines
moderate
are
pressure
particularly
increase
rare in the industry,
useful
where
is required.
the exception
p very
high
Such applications
being
LNG
either
for
gas flow
remain
a
relative1
plants.
i of 23.
DISCHARGE .
! of
TEMPERATURE
Discharge
LIMITATION
temperature
condensation
is limited
or compressor
(or
upstream
reasons
equipment)
of
gas stability,
mechanical
ga
resistant
limit. .
For reciprocating is usually
between
For centrifugal
.
temperature
2.4.
DESIGN
5. WEIGHT
a margin
and size
The use of vendors
for
6.
no margin,
industries
temperatures
of
but if. the flow
10 % is recommended
within
is coming,
in order
of these -production
we recommend
4 could
weight
of a centrifugal
oil console,
be used for
.
compressor
.
control
.
overhead
REFERENCES
of the compressor
catalogues
Figure
to ask the control
itself.
the discharge
the above limits
to
from
take
into
a productiol account
the
separators.
could
be misleading
a very
preliminary
compression
package
skid (aeroderivative
gas turbine
AND
(seal oil) USEFUL
LITERATURE
LUDWIG
Volume
3
Chapter
12.
6.2.
CAMPBELL
Volume
2
Chapter
14
xe
6.3.
GPSA
Chapter
JlY
6.4.
SSI Program
5
1979
as vendor
As the compressor and sometimes in estimating estimation.
including
room tank
manufacturer
cabinet
6.1.
ity
to be allowec
“C.
are used to maintain
slugs at the inlet
also the seal and lube
ely
used in gas and oil extraction
to 170/180
is constant,
only the size and weight
urn
temperature
AND SIZE
For weight
f0
gas outlet
MARGINS
separator possible
compressor
intercoolers
If the flow
ldl
the maximum
160 to 190 ‘C.
is limited
Normally
.
compressor
:
+ compressor)
catalogues
package the driver
the installed It is established
detaj
also indudc and gear box weight. for the
dr,
rOTAL
PROCESS
ENGINEERING
DESIGN
MANUAL
Revision
:
Date
:2/a
o
Page No :
cokPYEsso3.s rEP/DP/EXP/SUR--------------------
----------I II
.--
) -----------------
--------
-
3 E
B-w--
-
S hX -h
X .E
2” --.--e----w------
A4% --
---------------
i=T
I
__._._--------------------------
.-.-
--------
-.--------mm-
zu -!-
L
m----e---
-----------
---2 --
-----------
u m
C C _______-
----------------------.-
-----------
II .-E I :
7.3
.. CONDITIONS
SUCTION PRESSURE DISCHARGE PRESSURE
Pl = 6 P2 = ‘Y-
;;;
SUCTION
Tl=
C K
TEMP.
46 =3lq
SUCTION ACTUAL
2 PRESSURE
W =~OOooO KG/H V = 12.400 M3/H
FLOW ’ VOL FLOW
RATIO
PZ/Pl
= 2.33
32.34.
MW=
GAS DENSITY SUCTION =
AT 7-73
KG/M3
NOTES
STEP 1.
GAS PROPERTIES
2.
POLYTROPIC
3.
AVERAGE
PC TC EFFlCIENCY
d = MCP/MCP-1.99
4. DISCHARGE
= =
44.11 241
SEE FIG.
S=
1-l s
ESTIMATE
TZ 2 AVG
= = r
366 q3
K ‘c.
cc6 ‘c
OK /
Zl = 6*4&S = 0.4508 22 . Z = o-458
SUCT DISCH AVG
A
O.%O
TEMP
DETERMINE
BAR K
If =
l-2
5.
7.G
>
OPERATlNC
2 T2
k-c)
REPEAT STEP 3-4 IF T2 IS DIFFERENT FROM ONE USED IN STEP 3
I
, 6.
CALCULATE
GAS HORSEPOWE
GHP=2*R+W4~*(T2-Tl) MW
7.
CALC
SHAFT
PS = GHP
8.
ESTIMATE
l
GHP 3600
l
ESTIMATED
* (1 - F/100)
DRIVER
\c=iQ
KW
+ l/7
R = 8.314
KJ/KGMOLE
m
PS
=
\6S5
KW
F GHP<SOO K W 5.0 800010 MW 7.5 >lOMW 10
TM .96 -97 .98
POWER
l
PACKAGE
COMPRESSOR-DRIVER-LUBE NOTES
=
1)
HORSEPOWER
ELECTRIC MOTOR GAS TURBINE PS
9.
(I-
PS + K (1.14 + K)
PO PO
= (403 =
KW KW
K = 1.15 K = 0.02 TO 0.04 WITH GEARBOX
M
= @do=
KG
(SEE FIG 4)
WEIGHT
:
PROCESS
CENTRIFUGAL OR AXIAL COMPRESSOR
CALCULATION
SHkET
ITEM :. EK*PLc MO :
OPERATING
7.5
CONDITIONS
SUCTION PRESSURE DISCHARGE PRESSURE
PI = 6 P2 = I+
SUCTION
Tl=
TEMP
PRESSURE
46
‘C K
= 719 SUCTION FLOW ACTUAL VOLUMETRIC FLOW
w
=
L co oco
kg/hr
v
=
It400
m3/h
rMW =
DENSITY AT SUCTION CONDITIONS = 7.33
= 2.33
kg/m3
NOTES
1. GAS PROPERTIES
K bar
‘d = MCp/MCp
3. CALCULATE
=g
St.%-
STEP
2. AVERAGE
RATIO
i
- 1.99
DISCHARGE
TEMP I-I
=
Tlx
E-%-
= 362 = 59
T2
0 4. DETERIL!INE
OVERALL
Repeat 2 - 3 if T2 differ ‘5 from that used in STEP 2
EFFICIENCY See Fig 3
5. CALCULATE GHP
=
6. CALCULATE
GAS HORSEPOWER RxWx ,MW x3600x
Electrical 8. ESTIMATED
NOTES
I-
SHAFT
PS = GHP/f 7. CALCULATE
I 1
x (T2 - T1)
HORSEPOWER
kW
PS
kW
7g
x
DRIVER
=
R = 8.314 klkgmole
30%
f = 0.96 to r).97
POWER
PO = 1.15 x PS
(Motor
GHP = 23e&
PO
WEIGHT
=3qso
i+-=o
:
.
PROCESS
C,~.LCULATlON
SHEET ITEM :
RECIPROCATING
COMPRESSOR NO
:
Exlu?‘_
TOTAL 1
PROCESS
ENGINEERING
DESIGN
MANUAL
Revision
: 0
I
Page No :
TEP/DP/EXP/SUR i
-w-w---ROTART
-------w-q
CWCnLsoRs ;
(VOLUYETRIC)
: i -
: I I I
.
1 I I
CL*lIIIfUQALfIYs I
I
An0
l LOVLRS
/
_
I I I
I
I
I la00
1m
10 om
lwQ0 ACTUAL
FIG.
1
CEWERAL
RANGES
OF
APPLICATION
FOR
DIFFERENT
CDYPRESSOR
SUCIION TYPES
f LOW
( u)w[
”
PROCESS
ENGINEERING
DESIGN
MANUAL
Revision
:
0
Date
: ~/es
CWPRESSORS
TEP/DP/EXP/SUR
0.79
r --py
1 So
-
-.=
.:
DRY WEIGHT ESTIMATE CENTRIFUGAL COMPRESSOk
: _..;‘I.i . . . .1’._ .- :I__.:-..;--,.. _ : f; :-z.y -t ::: :-z-7,:: . 7. ; -~*.++:B.~.. --.-.v _._.-.
.-::..
FOR PACKAGE
c
Page No :
7.a
C
TOTAL
PROCESS
ENGINEERING
DESIGN
MANUAL
TEP/DP/EXP/SUR
.
8,
EXPANDERS
Revision
:
Date
:
be 2f8S
No :
.
I
,
.TOTAL
PROCESS
ENGINEERING
DESIGN
MANUAL
Revision
:
o
EXPANDERS TEP/DP/EXP/SUR
Date
bf85
1. APPLICABILITY I
For-both
the feasibility
a process data sheet conditions
Outlet
with and
2, DESCRIPTION
AND
horsepower
mechanical
energy
-
Turbo-expanders cryogenic
pressure
.
dew point
control
.
C3/C4
the expander
be calculated diagram
Thermodynamical
.
Expanders
which
It removes
is most often
energy
See Figure
is the
on Figure
energy
from
of the gas. The energy used to drive
a single
ethylene
gas which
results
is converter’
ratio
of the
actual
energy
\,
compressor.
I / /
processing,
etc...
removed
to
the
maximum
I :
depends
on :
-
inlet
pressure
-
gas composition
-
inlet
temperature
-
speed
a value content
of 80-85
at the outlet
gas must
% can be used for estimation of the expander
be free of solid particles
horsepower
figure
should
.
Turbo
expanders
.
Efficiency
Ij t
*-o
1.
discharge
estimation.
stage
.
-
,Maximum
to the laws of
removed
C2 recovery
maSs flow rate
.
a process
.
-
inlet
according
HBl HA efficiency
.
are OK.
HB HA
1
;
I I /
efficiency
=
Liquid
by computer.
efficiency
theoretical
.
in
horsepower.
accurately
is designed
let down
principal.
expander
Generally
1
to fill
recovery
.
Expander
be required
could be used for :
.
The
device
and temperature
which
will
NOTES
and aerodynamics.
in pressure
can
using a COLLIER
is a mechanical
in a drop
the engineer
and to estimate
estimation
systems
GUIDELINE
The turbo-expander thermodynamics
study
the basic information
caks for pure component
iiand
.
study and a pre-project
and water
of the manufactured
not however
be considered
varies
turbo
from
pressure
purposes.
See Figure
2.
10 to 30 % (weight)
(ice formation expanders
is prohibited). is about
12 000 HP.
This
as a limit.
can be used in series.
is affected
by the
variation
of the
design
flow
rate
See Figure
3 ior
an
I AC I I
,
I
I
TOTAL
PROCESS
ENGINEERING DE%N EXPANDERS
MANUAL
TEP/DP/EXP/SlJR
3. REFERENCES
AND
USEFUL
CAMPBELL
VOLUME
II
Engineer’s
guide
to turbo
I
Revision
:
0
Date
2/85
8.2
LITERATURE
.
expanders
HYDROCARBON
PROCESSING
APRIL
1970
Page 97... Turbo
expander
natural
applications
in
gas processing gas
offer
a way to conserve Use expander
processors
energy
cycles
for LPG
DOCUMENTATION
I.e. : ROTOFLOW,
MAFI-TRENCH..;
TECHNOLOGY
611 etc... PROCESSING
1970 page 105...
THE OIL AND
GAS JOURNAL
Jan. 23, 1978 page 63... HYDROCARBON Page 89...
recovery VENDOR
HYDROCARBON February
expanders expanders
OF PETROLEUM
iMay 1976 Page
What you need to know about
Turbo
JOURNAL
PROCESSING
Dec.
1
Page NO :
1974
.. t
TOTAL
PROCESS
ENGINEERING
DESIGN
MANUAL
Revision
:
(\
Date
: 2/nS
Page No :
EXPANDE-SS TEP/DP/EXP/SUR
FIGURE
PRESSURE
8.3
1
PA
PB
“f3l
“B
ENTHALi’Y
“A
PA inlet pressure PB outlet prasure
TA
Inlet temperature
HA
TB
Outlet
temperature
HB Outlet
TBl
HB,
Outlet
theoretical
Outlet theoretical temperature
Inlet enthafpy enthalpy
enthalpy
FIGURE
3
ESTIMATED PERFORMANCE FUNCTION OF DESIGN FLOW
FIGURE
AS A RATE
2
85 i:: 82 81 80 79 78 PERCENT APROXIMATE
PLANT
FLOW
RATE
MMSCFD
OF DESIGN
FLOW
RATE
TOTAL
PROCESS
ENGINEERING
DESIGN
MANUAL
TEP/DP/EXP/SUR
Revision
:
Date
:
Page ‘NO :
2J82 i
.
9,
FLARE
SYSTEMS
TOTAL
PROCESS
ENGINEERING
DESIGN
FLARE
TEP/DP/EXP/SUR
MANUAL
SYSTEM
Revision
:
Date
: 2,85
.
O
1. APPLICABILITY For
the
needed.
feasibility Required
information
Evaluation
.
Determination
of maximum
.
Flare
Design
.
Estimation
of height
.
PSV sizing
(not always
of number
KO drum
further
DESIGN
more
GUIDE
DEFINITIONS -
Relief
studies , a detailed
for either
.
For
2.
and preproject
and levels
of flare
relieving
required,
detailed
system
:
-
Vent system
or boom
is not
;
flare
length
design
capacity)
3 in DESIGN
and
design
requirements
l3LOU’DOU’N
consult
the
CFP
SYSTEXS.
I
GUIDE) relief
valve/rupture
disc downstream
piping
separator any depressuring the
valve,
pressure
piping
and separator)
a system
which
ensures
release
of
downstream
relief
common
the
II
AND
any pressure
includes
system
and type of tip required
on project).
specification
(normally
Flare
system
I , II 8
(and hence
depends
includes
system
-
flare
system
ON FLARES-VENTS-RELIEF
(see section
Blowdown
will include
of the
I’ of flare stack
and liquid -
study
design
and
depressuring
the combustion
hydrocarbons
piping
to
and separator systems
utilize
of hydrocarbons the
atmosphere
without
combustion -
Design
the
pressure
pressure
thickness -
the
Set pressure
design
through
allowable
is allowed
a safety
Usu‘ally
the safety
SYSTEM
ANALYSIS
This section
details
a feasibility
or preproject
.
A sysrem
economically
of
irems
device.
for external
to the Design
in vessel
Normal
is adjusted
J
the
to open
under
Pressure
pressure
during
accumulation
fire due to hydrocarbon
discharge
is 10 % but 20 % liquids.
For HC gas
of 5 96 is recommended.
the number
srudy and other
by consir
and calculate
AND GUIDELINES
how to determine
of
vessel
device
equal
increase
fires an accumulation 3. FLARE
the
1.0.)
at which
conditions.
maximum
Accumulation
to
(see section
pressure
service -
used
f
iipment
and
and levels
of tne required
flare
system
for
guidelines. can be protected
piping
~g it a~ a single
unit
when
calculating
against
overpressure
the relieving
capacity
most
r
’ ‘TOTAL iI
PROCESS
.
should
ENGlNEERlNG FLARE
DESIGN
Revision :
MANUAL
Block
not
be present
in the
system
so as to
relieving point- Special cases may warrant a car-sealed such arrangements should be avoided if possible .
:2/8S
Date
valves
Interconnecting system
piping
should
not
should
be of adequate
be of such
Page NO :
SYSTEM
TEP/DP/EXP/SUR
:
0
a size
size
that
two
isolate
9-2
‘a unit
open or locked
valve.
from
its
However
. and not
subjecr
separate
10 plugging.
systems
would
q-he
be
more
setting
there
safety
valve
economical .
ln specifying
the design
pressure
of the individual
items
and safety
valve
are two approaches -
Set
the
design
settings -
to protect
Study
the items
unexpected .
pressure
Consideration
as a single
should
Light
hydrocarbon
-
Heat
exchange
each
the weakest
“weak link”
-
of
link
system
limit
item
in the group initially.
the operating
be given to possible systems trains
independently.
Then
of items
This is preferable
as it avoids having
an
conditions.
abnormal
conditions
can reach low temperatures
may be bypassed
specify
resulting
viz : during
in higher
depressurization
than
normal
downstream
temperatures
.
-
Failure
of cooling
-
Production
medium
separators
It is often
required
the
of equipment
items
Consideration -
Relief formation
-
flare
system
temperatures
feed temperature, two or more eg : high
especially
separate and low
piping
The other
systems
systems
from
headers.
0°C
must
be kept
the flarelines.
may
This
be economically
apart
from
could
warm
moist
cause a system
desirable
to minimize
gases to prevent plug up the extent
of low
piping
backpressures
molecular
on the low pressure
composltion
streams.
e g moist
second smaller in corrosion
offshore.
temperature
By segregatrng the flows from high and low pressure sources into systems greater use of the high pressure drops can be achieved severe
-
to the
of ice within
Segregated
to provide
downstream
be given to the following
below
temperature -
may have a varying
or beneficial
should gases
can cause excessive
of some
systems
streams
may
CO2 or H2S is corrosive.
vent system to handle these rather
resistant
material.
two separate flare without imposing
warrant It may
their
segregation
be cheaper
than fabricate
from
to fabricate
the entire
system
a
TOTAL
ENGINEERING
PROCESS
FLARE
TEP/DP/EXP/SUR
Determination
of the flare
system
DESIGN
MANUAL
SYSTEM
and level
can be summarized
Revision
:
0
Date
: 2/85
Page No :
L
in the following
9.3
step by stel
analysis. 1. Does the facility
contain
process
areas with
LP compression
; atmospheric
separation
If so, consider
two or more
flare
distinct
pressure
levels
eg : HP compression
?
levels
if sufficient
limitation
is imposed
by the LF
section 2.
Does gas exist
at high pressure
be segregated
from
warm relief
consider
low temperature
3.
Identify
any corrosive
4.
Is a vent system
5. Identify
relief
required
links”
allowable
system
consider
them
into
links
a higher
to acheive
The
sizing
largest total
of every relief
compressor
or equipment
throughput.
Generally
For this, a full
system
fire generated
in identifying
the possible
of laterals
perform
a full plant
In some
cases, the resulting controls
may
have tc
“risk
I 1
vents etc... and consequently
vessels. (MABP
If only
1 or ,2 exist
the “weak within
the
= 40 % set) so as to incorporate
alter
the design
economical system,
pressure
two flare
it is necessary
to size the main
of upset
relief
conditions
levels.
I
load generated
I
is not necessary
can usually off the in a flare
loads
be judged first
separator
design
one or two cases that
flow
higher degree
will size the flare
drum
or a
of experience system
without
flaring back-up
I
of a
than the normal of the flare
II
the
depressurization
the sizing
A certain
Invariably,
or compression
by a simultaneous
do not dictate
and subheaders.
by inspection.
plant
system,
but
will
help
having
I
to
/
risk analysis.
to start
!
of the weak
than specifying
an idea of the maximum analysis”
Locate
its
load and conditions.
loops resulting
the sizing
- 29°C
10 % of set pressure).
or even
This may be supplemented
may influence
automatic
valves
of the flare
will be a full flow relief failure.
below
PSV anticipated
pressure
system,
itself.
case of the flare
electricai
flare
For the studies
vent flow
usually
relief
the configuration
is a listing
falls
regeneration
the same. This may be more
only and the flareline
to below 0 “C. If so, it must
if need to pipe up separately
of each
(MABP
balanced
pressure
headers neither
breathers,
i.e. : the low design
determined
be required.
and consider
the set pressures
Having will
sources
for tank
installing
will fall
I I I
headers
backpressure
in the process
on depressuring
gas. If the temperature
steel
on the PFDW
maximum
that
/ I / I
loads may be minimised equipment.
by using
ESD isolation
valves or
/ / I I
TOTAL 1 4. HEADER
DESIGN
FLARE
SYSTEM
SIZING
: STACK
to estimate
the main
flareline
and header
-
Design
flowrate
-
Length
of flareboom
-
Type of tip and stack
to be used.
DESIGN
TEMPERATURE
This has already
The choice
Page NJ 9.4
I
sizes based on .backpressures,
3 pieces of
of stack
been determined
AND from
MW
the previous
TO BE USED
(see section
and tip type will
section. 10 in Flare
obviously
Design
be dictated
Manual)
by the location
of the
under design.
stack
with
by the
plants
in remote
a conventional
radiation
occupied
areas,
pipeflare
height.
a further
reduction
type
pressure
could
in height sonic
Offshore
the
choice
vertical
stack.
economics,
The
location
eg : water
pressure
levels
lengths,
FLAREBOOM
under
computer estimate
program of radiation
AP 521. See Appendix
radiation
SUPERFLARE. 1.
loads
still
result
specif its
tip
often
entry
and associated
not to
tips
in order
to
support
for
a remote
or even on board
than
flare
stack,
MANUAL
between
pertainent
sonic
resulting or similar
DESIGN
flare
For non
in a tall
a Coanda/Indair
boom
is more
be determined
the stack.
in choosing
mounted
vertical
governed
each
platform
are used where
reduce
structure
by
stack/boom
weights.
SIZING
value
conditions level
round
10 in FLARE
however
levels,
of this
of wind
and
will
(15 700 W/m21
by using
these
bars) at the
(hereafter
thermal
area
complex 45”
Generally,
STACK
calculation
a variety
more
between
radiation
or stack
allowable
A detailed
(2-5
- FLARE
flareboom
maximum
depth.
sterile
(see section
considerations
allow
by reducing
tip
decision
of the stack
high flaring
or an integral
structural
height
to use a remote
be high as 5000 BTU/h.ftZ
is somewhat
or similar,
sufficient
can be achieved
flare
of each tip type). flare
The
For cases where
discussion vertical
tip.
on the designated
this figure
stack
high
areas it -is usually
limitation
in a short
The
:2/85
(
,MW
or height
of stack
For onshore
4.3.
temperature
OF TIP + STACK
plant
Date
0
:
FLOWRATE
TYPE
:
AND TIP CHOICE
are required
42
Revision
. I
information
4-l.
MANUAL I
I
TEP/DP/EXP/SUR
In order
ENGINEERING
PROCESS
termed
flare)
tolerable for
length
on the platform
vertical
or inclined
and temperatures For
feasibility
can be determined
is determined
using
or surrounding flares
the
preprojects, method
area.
on or offshore
can be performed and
by the
using
the
however
an
as detailed
in
OESlGN
FLARE
TEP/DP/EXP/SUR
Recommended
Radiation
levels
MANUAL
SYSTEM
are given
below :
Allowable radiation 6tu/h.ft2
I
Condition
1 I
I
I I I
I I
I
I I I I I I I
Areas where personnel may be located and expected to perform their duties continuously
I I I i
1000
Areas where personnel may be i located from which escape is I possible and shelter is ; attainable
2000
I
I
I
I I I I I I I
Areas where equipment is i located and personnei are not I normally present during operation, but if present im1 ; mediate shelter is available I
I
I
I I I I I I I I 1
Infinite
f I 1 minute
f I I i
*
I I
i
)I I
5 seconds
I I
(Emergency flaring only)
‘>
I
I
3000
i I
I I
_I
I
I Areas where personnel are not I permitted during operation
I I I i The
above
figures (
should
radiated a)
0
t I I
I I
are
250 BTU/hr be noted
and math
1000
I I allowable
maximum
radiation
”
I
t
I I
I
I
i
Helideck
radiation It
5000
i I I
intensities
inclusive
of
solar
ft2).
that
the
numbers
following
recommended
values
of F - Fraction
of heat
at the tin. I
Pioe flare
: Low MW gas F =
0.2
Ethane
F=
0.25
Propane
F =
0.3
Velocities
-
max at design
-
normal
relief
continuous
=
0.5 M
=
0.2 M
I
I i
b) Indair/Coanda All gases c)
,ttardair Having
calculated
the design
flare
F
=
0.1
F
=
0.05
the flare
IMach .
1
I
:Mach 1 length
based on radiation
fates and tip type the main
header
:
I
I
I
’
I
Exposure period
analysis
and established
both
can now be sized. I
PROCESS
ENGINEERING
DESIGN
MANUAL
TEP/DP/EXP/SUR 4.4.
HEADER The
SIZING
major
velocity.
criteria Flare
on the plant Sizing
governing
headers
safety
must
the
sizing
of the
header
be both large
enough
to prevent
valves and to limit
gas velocity
link”
to MABP
“weak
with
respect
been done when determining pressure
tolerable
2) Calculate
A
the
For pipeflare
the levels
P across
the flare
3) Estimate
tips use :
generous
4) Calculate
1 I: I
levels.
of relief).
values.
design
on load.
Fluid
seal
0.2 - 0.5
psi
(0.014 - 0.034 bar)
0.5 - 1.0
psi
(0.034 - 0.07 bar)
flare
seal of piping
headers
from
the tip
are complex
of the relief
to the
should
Where
IN STACK
the estimated
KO drum.
and rarely*straight).
gas
of required
pipe id based on maximum
be one or two sizes less than
=Pf
for isothermal u;
+
1
= upstream
conditions
2
= downstream
P lJ
= pressure = veloclry
V
= specific
This calculation
requires
bar (a)
KO drum.
fL
39.4 (
tin
d
+
friction
f
=
moody
L
=
equivalent
d
=
pipe id
length
m/s vol m3/kg a degree
of trial
flow. LIMIT
The Conison
flow :
P2 V2
relief
the tip diameter.
TO 0.85 IM;AT DESlCN FLOW. IfiI D calculate the A P from tip to flare
is recommended
:
flare
K = CP/CV T=K
diameter
6
For sonic type
(0.034 - 0.14 bar)
length
margins,
flow.
psi
The
equation
upstream
0.5 - 2.0
estimate
5) Using
have
tip
This will give a first VELOCITY
should
This is the maximum
V sonic
stack
(this
Flare
the sonic velocity
1
on safety
will be 2.0 to 5.0 barg depending
the equivalent
(Allow
I
backpressure
and noise to acceptable
tip for the relief
Molecular
Ii
excessive
and gas
in the system.
tips the backpressure
!’ . I .. . I : I
backpressure
procedure
1) Identify
1
Fe
and error
as ul = f (p1)
uz Ul > factor m inchs
x 10
-5
TOTAL
PROCESS
ENGINEERING
DESIGN
FLARE
the PI (talc)
is adequate
ie is PI
allowable 7)Once
satisfied
calculate
with
along
the “weak
9) If the project static
at the relief
drum
(talc)
approaching
the
drum-tip
and decide
line
Date
: 2/85
0
Page No : 9.7
if the stack
+ header
maximum
upstream
and repeat
proceed
back
the AP
up the
diamete pressure
talc.
flare
header
ant
of line diameter. adjusting
link”
has been satisfied.
criteria
requires
the
the diameter
the headers,
backpressures
EXAMPLE
drum
? if so increase
the next section
8) Continue until
at the plant
:
SYSTEM
TEP/DP/EXP/SUR
6) Examine
Revision
MANUAL
sub headers calculated
flowrates
and laterals
as necessary
if sources
can be estimated
from
disappear
the main
line
above.
:
‘I > ‘< l-2 b+
1. Flare 2.
design
Weak link
3. System
is based on vent flow from
in system must
backp,ressure 4. Size line from 5. Check
drum
is set by PSV at source
be designed at point
from
for
(3) of more
tip to drum
to point
source
a design than
(1) 1
(2)
flow
from
source
(I)
not
giving
1.2 barg.
(L = 150 m) to give P drum
1
0,5 barg (say) size line
(3) (L = 100 m) to give Pl < 1.2 barg.
that source (1) can flow from
2
(1) to (3) with pressure
I
drop available. I
I -
’ TOTAL
PROCESS
FLARE
TEP/DP/EXP/SUR
I
DESIGN MANUAL
ENGINEERING
SYSTEM
Revision
:
0
Date
: Z/85
Page NO :
9.8
I NOTE
: 1)
Laterals
--->
sub headers
as the system Max velocity
2)
When
. 3)
progresses
temp
for each section. at
must
to the tip.
A P for
A T vs d P profile
a
headers
specific
flare
yield
points
more
in
the
in diameter
duration
systems
reliefs
isothermal
For high source
will
increase
,
in a line is (MACH 0.7 for short
calculating
assumed
--->
pressures
accurate
system
to
only. flow
with
is
low ,MU’
results,
i.e. adjust
account
for
A
P
occured.
I
5. FLARE
KO DRUM
A flare
KO drum
SIZING is provided
to drop out and collect
the liquid
part
of the flare
vapours
in
c\rder to :
I
-
prevent
-
to minimize
‘I 5.1.
to recover
at the base of the flare
the risk of burning and reclaim
DESIGN
I
-
I
-
liquid
I
valuable
(golden
product
boom or tower
rain) emerging
from
the tip and falling
on
I
materials.
CONSIDERATIONS
separate
knock
installed
i.e. .* an HP KO drum,
cold line
I
accumulation
personnel -
i
liquid
vapour
out drums
lines
(i.e.
to a “warm”
drum
call below design. -
FLARE
-
Mist
are generally
LP KO drum,
can be introduced
providing
the resultant
eliminators
SHOULD are
not
for each level
LLP
< 0°C)
This precludes
KO DRUMS
required
immediately temperature
upstream in the drum
the need for two independant
be installed.
system
drum
BE HORIZONTAL to
of flare
of inlet does not
drums.
AT ALL TIMES. Min
design
pressure
of
drum
is
3.5 bar (g) 1
-
Heating
coils
should
residual
liquids.
LIQUID
DROPLET
be installed
Typical
in flare
is to maintain
a T min
I
I
I
Recommended
particle
VERTlCAL
FLARE
INCLINED
BOOM
REMOTE I
SIZE (per API 521)
FLARES
sizes are : 150
(offshore)
> 45”
‘150
”
< 450
400
”
600
KO
drums
= 4°C
to
prevent
freezing
of
TOTAL
PROCESS
ENGINEERING
DRUM
MANUAL
SYSTEM
FLARE
TEP/DP/EXP/SUR
5.2.
DESIGN
Revision
:
o
Dare
: 2,85
Page No :
i
9.9
SIZING
Based
the above
on
method
outlined
For a flare
design
in section
KO drum,
drum
i.e. : utilise
large
diameter mounted
highter
drum.
2.0. VESSEL
the normal
as much drum
nozzles
considerations
liquid
level
consider
on the head.
This
is especially
KO drum
can be sized
using
the
DE.SIG,\I.
space as possible
results
This
the flare
should
be kept
in the lower
for the vapor-liquid
using
a split
will
maximise
useful
offshore
flow where
of the
de-entrainment.
arrangement
the L/D
part
ratio
weight
with
and give + space
If a the exist
a smaller
are a major
concern. An LCHH wellhead 6.0.
RELIEF 6-l.
will
normally
in the flare
drum
to initiate
a plant
shutdown
’ .
shut in offshore).
DEVICE
SIZING
(For more
detail
see API 520, 521) -
GENERAL - Safety
valves
backpressure - Rupture
are
either
termed
balanced
or conventional
depending
upon
the
and cannot
be relied
limitation
discs are less robust
on to function 6.2.
be installed
accurately.
than
an equivalent
It is recommended
that
safety
valve
rupture
discs are avoided
BACKPRESSURE - Backpressure
exists
. flowing
backpressure
blowing
in two forms is the
to the relief
off
: pressure
on the
discharge
side
of
a PSV that
is
system
. superimposed
backpressure,
or
discharge
side of a PSV caused
static
backpressure
by another
relief
is
source
the
pressure
in the system
on
the
venting
to
flare - For conventional superimposed allowed 6.3.
LIQUID
the
or flowing
is
for without
a reduction
,Maximum 10 %.
Allowable
For balanced
in the valve
Backpressure
relief
valves
(MABP)
for either
up to 40 % can
be
capacity. ,
RELIEF
The formula
A =
valves
for sizing
liquid-relief
valves
is :
gpm ins
27.2 Kp.
K,.
K,
a
PROCESS
FLARE
4;* 9
ENGlNEERtNG
DESIGN
MANUAL
SYSTEM
: 2185
Date
TEP/DP/EXP/SUR
9.10
,/Where :
the
I’
I
A
=
Effective
discharge
gpm
=
Flowrate,
U.S. gallons/min
c
=
Specific
Kp
=
Capacity
correction
Pd
=
Relieving
pressure
K,
=
Capacity
correction
factor
(from
figure
6.4)
K,
=
Viscosity
correction
factor
(from
figure
6.3.)
6.4.
VAPOR
gravity
area,
ins2
at flowing
.
temperature
factor
(from
minus
figure
constant
6.5)
back pressure
RELIEF
The formula
for sizing
vapor relief
W
A=
c
K
is : Ti!
pl
Kb
r-
1M
Where : h
e
=
Relief
T
=
Inlet
c
=
Coefficient
(from
K
=
Coefficient
of discharge
PI =
flow, lbs/h vapor temperature,
Upstream
=
i
w
factor
“R
figure
pressure,
Compressibility
6.1, 6.2) (0.975
psia.
unless vendor
Set pressure
data
available)
1.1 for blocked
outlet,
CV failure
or 1.2 for fire .plus 14.7 psia Kb
i:
6.5.
Capacity
=
correction
Molecular
weight
M
=
RELIEF
FOR GAS EXPANSION
A=
If
As
factor
(from
figure
6.6)
of the vapour DUE TO FIRE F’ =
&
0.1406
Tl.25
CK
T0.65G6
tc
?f
A
=
effective
A,
=
exposed
discharge surface
area of valve
area of vessel
ins2
T
= 1560-T
ft2
T
= temp.
pressure
)e
6.6.
STEAM
RELIEF U’
ir\s 1
A= 50 PI
Ksh
.“R
at relief
TOTAL 1
PROCESS
I
TEP/DP/EXP/SUR
PI
=
.
ENGINEERING
DESIGN
6.7.
FLARE
Set pressure
x 1.03.
correction
RELIEF
STANDARD
The following
table
discharge
(ASIME Power) (ASME Unfired
VALVE
factor
table
ORIFICE
may be used
SIZES the relief.valve
as in paragraphs
Effective
*
Avoid
size based
6.3. through
6.6.
Normal
size
Area
Designation
0.110
lD2
E
0.196
lE2
F
0.307
1 l/2 F2+
G
0.503
2C3’
H
0.785
2H3
J
1.287
, 253 or 3J4*
K
1.838
3K4 or 3K6
L
2.853
3L4 or 4L6
M
3.600
CM6
N
4.340
4N6
P
6.379
4P6
Q
11.045
R
16.000
6R8 or 6R10
-r
26.000
ST10
using 2 l/2 inch outlet using 2 L/2 inch inlet
9.11
vessels)
flanges
648
(F and C orifices)
. l
: 2/85
D
Avoid
Page No :
6. I.
for estimating
areas calculated
Date
sq. inches
l
0 I
Nozzle Orif ice letter
:
SYSTEM I
- superheat
effective
Revision I
or 1.1. Ksh
MANUAL
flange
(3 orifice)
’
upon
the
TOTAL
PROCESS
ENGINEERING FLARE
DEStGN
Revision :
MANUAL
SYSTEM
Date
TEP/DP/EXP/SlJR . REFERENCES
0
I
Page No :
1 9.12
: 2f85
+ LITERAIURE .
7.1.
DESIGN
GUIDE
CFP MAY 7.2.
7.3.
Flares-Vents-Relief
systems
1984 - TEP/DP/EXP
API
520
AP1 i4c
API
521
API
Det Norske
and Blowdown
Veritas
Norweigen
Petroleum
conceptual
designs.
0.99
I4E
.
: T&hnical
Notes
: Guidelines
Directorate
0.91
0.97
0.96
fixed offshore
0.95
0.94
0.93
z
installations
for safety
0.92
a.91
evaluations
0.90
0.19
of platforn
011
259 x7 301 124
II5 341 157 170 315
311 350 MI 170 379
39s 405 41s 421 411
415 425 415 UJ 450
440 4sO 415 463 470
466 47J 460 417 492
311 396 a3 409 416
uo 445 4Sl
173
2: SI? 510
91 5%
2
47s 410 415 490 49s
497
447
4% 461 470 475 4IO
iii 516 590
E (46
A?2 411 UI 470 419
452 465 47s 49J $12
470 410 492 III S10
415 496 R
:z
J20 510
JSO $11
si,
it:
z $70
3;
551 SI?
570 I91 620
NJ 608 630
597 620 640
U? 660
653 670
Z
no
SlO Y6 574 597 bI9
z: 591
617 670 697
-
2: c17 665 690 7,)
467 472 471
iI 490 497 ii:
492 492 493 49s 497
:F: JIO 510
JO0 $05 510 JI6 J13
110 JII 315 II6 590
513
J9S
593 602 b10 625 6II
610 611 6X
uo 705 7:s 744 759 771 795 II
610 611 65s 676 692
615 64s ii: 704
661 6II 710 721 743
701 713 751
719 742 761
757 710 7VJ
:9
.I
TOTAL
PROCESS
ENGINEERING FLP.RE
TEP/DP/EXP/SUR
ANQ
DESIGN
MANUAL
.
. .
Revision
:
Date
:2/8S
0
Page No :
RELIEF
9.13
TOTAL 1
PROCESS
I
TiP/DP/EXP/SUR
ENGINEERING
DESIGN
MANUAL
Revision
:
Date
:
0
Page No :
AND RELIEF
FLARE
2/85
9.14
0.6
0.4
R=
REYNOLDS
NUMBER
I
v.
GIGE
BACK
PCIESJURE
8ACK PRESSURE. = sET PREUUaE
PSG ps,c
0
6.4 -v
ariable
.Focror
Balanced (Liquids
or
I(.
Constant
for’ 25 Btllowr
Back-Pressure
IO
I 100
~JOTF: The above curve rcprcxnts a compromise of the values recommcndcd by a number of rcl~cf.valve manufaclurcfr. This curve may k used when the mate of the valve is not known. When the make IS known. the manufacturer should bc consulted for the corrcct,on factor. Figure
s
NOTE: The above cent overprcssurc. change in orifice pressure. Above change
in
I
25 30 OvERPRESSuRE
35
rg
45
50
curve show that up to and including 3 per capacity is rllcc~cd by tbc change m lift. th dinhrrre cocficicnt. and the change in over 2S prcenr. capacity is rffccrcd only by th
overprenure.
Valves operating fore. Overpras~rer
at low ovcrprc~~ure~ of less than
tend IO pcrccnl
IO ‘chatter”: Ihcrc should be avotdcc
Siting
Percenl Overpressure Safety-Relief
on Valves
figure
G 5
.C opacity pressure Valves
Only)
--.
I
IS 20 PERCENT
-
Correction for ir.
Liquid
Relief
Foctorr and
Service
Due
to
Over
Safety-Retie
TOTAL TEP/DP/EXP/SUR
f
PROCESS
,
ENGINEERING
I
DESIGN
Revision
MANUAL
AfJD RELIEF
FLARE
:
0
I I
Page No :
I
Date
: 2/85
9.15
I
0.80
0.60 ’ ,
I
I,.
0.50. 0
5
IO %
GAGE
I5 BACK
20
2s
30
BACK
PREWJRE
d.6a-VariobIe pars
and
or Constant Gases)
Back-Pressure
Sizing
40
PRESSURE,
PSlG
. 50
4s x
= SET PRESSURE ps,c
,oo
.
ore: The above curies represent a compromise of the valuer recommended urcd when the make of valve or the actual critical-flow pressure point mown the manufacturer should be consulted for the correcrion faCfOr. TheA curves are for set pressures of SO pounds per square inch gage and )w pressure for a given set pressure. For subcritical-tlow back pressures IUS~ be consulted for the values of Ke igvre
35
Factor
K.
for
by a number the vapor
above. bclo~
for
They
of or arc
limited IO back per square inch
SOpounds Bolonccd
relief valve manufacturers gas is unknown. When
Beii~ws
the
and may make is
pressure below critvzalgage. the manufacturer
Safety-Relief
Valves
(Vo-
0.8
0.6
0.4
,.
0.2 I 1
0 0
20
IO
30
40
SO
60 BACK
Q/O ABSOLUTE
F igurt
C*6LC
onstonc Only)
Bock
BACK
Pressure
Sixing
PRESSURE
FOCIO~
= -SET
K+.
For
PRESSURE
Conventional
70 PRESSURE,
80 PSIA
+ OVERPRESSURE.
Safety-Relief
4 ’ 100
90 PSIA
Valves
(Vapors
’ loo
ond
=”
Cares
loo
APPENDIX A SAMPLE CALCULATIONS A.1
FOR SIZING A FLARE STACK
General
I26
For Mach low:
A.2
In metric
Exrmple 1: Sltlng I Flare Slack Ualng Ihe Simple Approach
In Iha r~amplc. Ihe basic dalr MC aa lullows~ The matercal llowtn~ II hydrwtbon vapor, 7he flow MC. W. IS IUU.WU pounds per hour (12.6 kilo~lrmc per c(c. ond). The wcagc molcculw wqhl ol Ihc rrpoo”. M. it 46 I. The llovint ~emptrr~ure. r, II 760 dcgwes Rm~hc (300 F) 1422 ktlrinc (I49 C)]. The hcaI of combuwon is 2I.w) ttrilish Ihrrmal uniIt pee pwnd (5 x IO’ kilujoulcs pc, kilqtam). Tbc ratio 01 the spccilic herIt m the gas. h. is I, I. The llowinl pte$su~e II Ihe llare lap is I4 1 podnds pet yurrc mch rbsalulc (101 ,I kiloprurls abroluIc). Ihc dcqn wind vclocily is 20 mdtr pe, hour (ZY 5 ICCI per ucond) (52.2 kilomeIc,s pc, hour (rpptuaimalrly ll 9 mc~e,c pa wcond)] A.2.l
CALCULATION
The Msch I 4 3 I. Ilcm
OF FLARE
numbo I).
OlAUETEtt
is dcwminrd
II
follu~
(UC
Math In “WI,,C
um~r.
Mach For hlrth
~rantlr~cc
- 0.5. the flare
diamcIo)
dinmeler
is calculaIcd
II fol.
d’ - O.lJY7 d - 0.95 fool (inside diwnclcr) unw.
this ~rrnsla~ec
IO:
d’ - 0 0~25 d - 0.29 meIer (inside A.P.2
CALCULATION
diameter)
OF FLAME
LENOTH
Tbc heal IibetaIcd. Q. In British Ihrrmal units pef hour (kilowalls). II calculrIed as fallows (we Fiauw 6A and 66): Q-(100,~)(21,5oU) - 2.15 x IO’ BrtiIish In mwic
unilt.
Ihr#mll
lhis ~~rntlatcc
units pa
IQ I-----rL,,,
hour
IO:
Q - (I2 6)(50 x IO’) - 6 3 x IO LilowaIIt From Figures 6A and 6D. lhc ft~mc fern (52 mclcrc) (see Finwe A.1). A.2.2 CALCUtAllON CAUSED BY WIND CALCULATION)
IcngIh.
L. II I70
r --------I)-----
OF FLAME DISfORflON VELOCITY (SIMPLE
flow ,aIc I, dewmined
Fbutr
A-l-Obnm4bnrl
Mrrmur
lot siring
I FAIR
dwnrItr
suck
-4
II follows: “‘i%$
IO:
- (II bl)(lO”@
- 0 2. Ihc ll.,c
WIND--.
(1.1)(46.1)
d’ - 0.2U9 d - 0.46 ~CICI (Inside
The vrpor Ihl,
JT
o.2 - (It.6i)(‘o”~
Tb~r apPendi ptocnac ca~mplcr 01 Ihe Iwo methods IoI win# 1 the ctark baud on Ihe tlltc~~ of IadibIion. The IWO melhods arc the “simple” apptoach prtunlcd in Section 4 rnd Ihc mole tpcc~fic apptorch usin) Brauc~owki rnd Sommtr’e melhod. HeiRhI and lo. cation should alu, be contidcrcd. bated on tar dirpruon il Ihc flame I) eatinguishcd (ICC 4 4.1.4).
“F
G
I, c.lculalcd
- 333.9 rc~ual ., lot
In mewic
unils.
cubic
lhis t~rnslrtcs
feel per wcond
The llwnr dlrionion uusrd by wind wlociIy Ilied us lollowr (ICC Figure 7):
II c~ltu-
- Ill9 feet per second In melric
IO:
Iowl:
unii~.
thls wrn~lair~
IO:
!iID
$‘~
flow
- (I2 b)(g) - 9 46 BCIUI
(g) cubic
rne~ct,
per tccond
fhc lollow 4):
u’-$eig
fl~rr tip CIII rclaily. U,. may be delrrmined I( (ICC A.3.2 lot ~no~hrr melhod ol calculaainl
u,-
Mow yyjl -i
For Mach
- 0.2.
- 56 9 McCoy FOI Moth
..
pa
P 2. -. ‘: . .
second s w
- 0.5. u’-d& 4 - 411 ICCI per second
0
lo 577 t;; oz ..
0’.R”4 II” 160’ - 7e’ 4 tI*l
zy .-0.12
- 21.600 - 6084
tl”
ZAy - (O.S3)(52)
- 19,Slb II’ - I40 feet
- 11.6 nw,era IAl
- (0.72)
t/ - I40 - H(60) - I IO IceI
(II)
- 37.4 “,LlC” In mcltic
AZ.4
.
CALCULAllOH STACK HEIOHT
OF REOUIRED
R' - 45.7 - H(lI - 27 0 mclrrs
unilt.
thir lrrnrtrlcl
FLARE
II’-
A.I.1.) R’ - alH(44.0) - 23.7 mclcrs D’-R”t It” 48.9' - 23.7' 4 ti” H”
- 2191.2 - X4.7 - 1829.5 H' - 42.8 mclcn
II - 42.8 - H(I8 - 33.1 mtltrr AI Mach
- 0 5. If ii calculated
2) 11 follow:
tl’ - II + CIAy R’-R-HAS
In melric
unils,
thir Irrnslalo
lo:
(kc
EAy
- 90.1 Ied
IAs
- I22 4 feel
A.2.1.) R’-
HO-
H(l22)
- 89 feel D’ I R” + ,,‘I MOJ - 69’ i II”
- 48.9 melcn
H"-25.600-7921 - 17.679
The physkal rrrrngcmcnl shown in Figure A.1 ir ihe buir of the followinS calculations. Al Mach - 0.2. the flare srrck hcilhr. II. is CIIN. lad .s fulluw
XAy
- (0 51)( 170) - 90.1 ICCI
IA,
- (0.72)(170)
II' - II * HAy
- I21 4 ICC1
R’-R-H&
If’ - I12 feel
ti In mcrric
units.
this rranslaro
- 1443
feel
CAy - 2; 6 mcltrr
(fee A.2.1.)
Lb R’ - I50 - H(144.3) 14
7a
IO:
II’ - It + Hby R’-R-Hbr
'261 - S9.J ICCI C&
- Ill - H(PO) - all feel
(kc
A 1.1 )
- 11 4 nILlen
II-‘-
- 119
1391.2 - lf162.2
- 40.1 - H(27.6) - 11 melcri
H t HAy
CAy - 18.2mclcra &lz - 44.2 mclen (See
II” t n”
II’ - 40 8 mcten
it'-R-HAS
For the basis of the calculalionr in rhlc section. r&r lo 4.4.1.3. Rtfcc IO Figure A-l for dimcnrional refer. cnces. lhc dcrign buis is II follows: The fraction of hcrr rathated. F. is 0.3. The hemI libcrrtcd (we A.2.2), Q. As 2.15 * IO’ British rhcwnrl uoirc per hour (6.3 x Id kilurrlts) The marlmum rllorrblc radiation. K. II 150 kcl (4J.7 mclcn) from Ihe flwc slack Is 2000 Britl#h thermal units per hour per square fool (6.3 kilowtta per squam mclcr). In rqurtion (I) from Secllon 4, wsume t - 1.0. The disrwxc from the flame unlcr IO the Srrdc.kvcl boundary (that is. the object being considered). D. ir lhcn crlculaled II lollow
D’R”4 4a 9’ - I7.d
I/
IO:
*
4)
Table 1 INTRODUCTION
’ il
of Contents
.......................................
.
1
2 BASIS OF THE STUDY ................................. 2.1 GAS COMPOSITIONS ............................... 2.2 COLD VENT ........ ................................................. 2.3 H2S CONCENTRATION MONITORING
2 2 ;
3 RESULTS _....._........__....-..-........*...--.....
4
4 DISCUSSIONS
5
_.._.....-.-.._._...-.--...-.......--...
5 OPERATING EXPERIENCE
...............................
6 CONCLUSIONS AND RECOMMMDATIONS
i
...................
8 9
1 INTRODUCTION The Welton Gathering Centre process plant is provided with an incinerator for disposal of excess associated gases and relief gases. During upsets on the incinerator e.g. fan failure or a plant initiated trip, the incinerator is isolated and the gases are disposed of through a cold vent via a bursting disc arrangement (see Fig 1). The gases routed to th e cold vent contain high levels of HZS and adequate dilution of this component with air is therefore required during dispersion for safe disposal. The option of replacing the existing incinerator with a new and larger one, means that the cold vent would still be required. Dispersion calculations were therefore carried out by Group Environmental Services (GES), London to confirm that safe disposal of the vented gases could be achieved. Detail6 presented
of
the atmospheric dispersion below. The following areas
study and results are covered :-
are
li
I /
Ii ! 1;
1 / i
-
basis of the study results of the dispersion modelling. discussions of results operating experience with the cold conclusions and recommendations
1: vent
I I, i I
II
i
j/
2 BASIS
OF THK STUDY
The dispersion Environmental calculations 2.1
calculations were performed by Group Services (GES) in London. The basis of 1 is given in the sections following. ,
GAS COWOSITIONS
The composition atmosphere can
I 1
I 1,
Ii
II ’ \! !
-I I I 1
of the be wide
gases that could ranging because
be vented :-
to
the
the Welton G.C. receives crude from a number of wells at varying flows and varying H2S content. Hence the amount and composition of the gases normally produced varies; - the relief gas composition which could superimpose normal flows vary depending on the relief scenario. Accurate prediction of the relief flow and composition not always possible.
on is
Therefore for the dispersion calculations reported here, a number of vented gas data compositions were prepared from two sources (Table 1) :* . - these were extracted 1) TLC Oriainal Desian C!mDosltuul from the Incinerator Work Pack 18, Vol. 1. They were based on the design wellfluid (C-site) and still represent the sourest gases that could be obtained from Gathering Plant HP/relief header. Calculations for the following cases were carried out gas and HZS flows, Gas I; a) Case 1 - Highest Gas A; b) Case 2 - Lowest H2S concentration, Gas E and c) Case 3 - Lowest H2S flou6, flow, Gas B. d) Case 4 - Lowest total
Ii I! / f
these
II)
a preu revised s&ign ca6e~ - these are based on the Welton Upgrading design material balance and represent condition6 in the plant when production from C site is diluted by production from the less Bour The combined.HP, LP and acid wells (A and B sites). gas stream compositions were used for the dispersion calculations. The following ca6es were considered :of normal flows in the a) Case 1 - based on the total gas headers; flow based on 300 BOPD; b) Case 2 - startup to Case 2 but with twice the H2S c) Case 3 - similar This can be considered as starting up concentration. 2
with production from C-site. d) Case 4 - based on normal fire relief flow in the gas 2.2
flows superimposed headers.
with
COLD VENT
The cold vent is a 16 inch pipe erected vertically with Detail dimensions 6 inch top section acting as a nozzle. of the cold vent as used in this dispersion study are shown in Fig 2.
a
Process gas is normally isolated from the cold vent by means of four bursting discs - two in use in series and two spare, as shown in Fig 1. Should these rupture, a common alarm signal is produced in the control room and the incinerator is tripped which in turn causes a general plant shutdown. Thus the duration and quantities. of the emissions is minimised. 2.3
HZS CONCENTRATION
The following HZS concentration vent :-
were selected dispersion
a) At positions in the plant manned, of which the following
b) At grade level Gathering Centre areas. c) At farm the Barfields The
tower
co-ordinates
for
the these
above were
of
for monitoring gases from
grade which selected :-
the
could
the cold
:I
be
.’ !I
- 14.9 m - 13.6 m - 9.O'm - 12.5 m
at various perimeter
houses in farm.
‘:!I
MONITORING
locations during
Crude stripper Amine contactor Crude tanks Incinerator
i ‘.t
locations fence, car
near
;s within the Welton park and workshop
vicinity
receptors
and are
in
shown
r
I
Table
1
:I
particular, in
j
1.
: 1
,
3 RESULTS Details extract results quoted quoted
of the results are given in a GES memo, Ref. 2 ; an of the results is given in this section'. The of H2S concentrations at various locations are in mg/m3. To convert these figures to ppmv then the figures should be multiplied by a factor of 0.7121.
Tables 2 - 9 show the maximum ground level concentrations for a range of weather condition6 and the cases specified. The wind has been arbitrarily set to SW, so the location of the point of the maximum ground level concentration is of no significance, but the distance from source is of use. at the seven sites Table 10 - 17 shows concentration specified for the same range of weather conditions and the However, in these tables, the wind same eight cases. direction has been deliberately chosen to place the Thus each specified site directly downwind of the vent. concentration represents the worst possible condition at each site. The result presented in the Tables 2 - 17 are the 3 minute average concentrations at the receptors. To extrapolate the 3 minute average concentration to longer time average concentrations, the following can be applied :,
cx = where
Cp * ( 3 / TX ) **0.2 Cx is Cp is TX is
concentration the 3 minute the new tim,e
Thus, for a 15 minute average concentrations Similarly, for 0.72. factor is 0.36.
average for time TX average concentration for average concentrations.
average concentrations, the 3 minute have to be multiplied by a factor oi an 8 hour average concentration, the -:
For time average concentrations of less than 3 minute, the However as a guide, a above correlation does not apply. similar approximation to that made for odour nuisance investigations (where the 5 second average concentrations to convert the 3 minute Thus, are relevant) can be used. averages to 5 second averages, the results in weather category A should be multiplied by 10, and the remaining weather categories should be multiplied by 5.
4 DISCUSSIONS
This Section diScU66e6 the interpretation of the results given in the above section. It must be stressed that the interpretation of the results and inferences made here concerning the H2S level with respect to safety, occupational health and nuisance6 are mainly those of the author. Advice from Group Safety and Occupational Health was obtained verbally and is incorporated. The
following
observations
are
made on the
results
:-
a) The odour threshold for H2S is d.00066 mg/m3 for 5 sec. average time. Tables 2 - 9 shows that the 3 minute average ground level concentrations (1/5th of 5 second averages for most weather categories) exceed the odour threshold. The use of the cold vent would thus result in odorous emission which would be perceived at fairly remote locations e.g. the Barfields farm, when the wind is blowing in that direction. It is noted that there are no evidence emissions due to H2S at low level are complaints relating the two may still
that odorous a health hazard, be received.
but
b) The cold vent facility is provided with two bursting disc installed back to back in the duty line with a parallel spare set provided. Should these rupture, an alarm signal is produced and the incinerator.is shutdown. The latter also causes a general plant shutdown thereby minimising the amounts of emissions. The release of H2S containing gases through the cold vent is therefore restricted to the HP/Relief header depressuring,or the depressuring of the separators in the HP gas blowthrough scenario. It is not possible to quantify these periods. c) Tables 10 - 17 show the 3 min average the seven particular receptors specified; odour threshold is exceeded.
concentrations in all cases
at the
If
the concentrations are adjusted to give 8 hr. time interval averages by multiplying by a factor of 0.36 then in some case6 the Long Term Exposure Limit of 14 mg/m3 is exceeded. This occurs mainly at elevated receptors and in particular the crude stripper and the amine contactor/regenerator.
If
the 3 min average 15 min average value Term Exposure Limit receptors.
concentration by multiplying of 21 mg/m3 is
5
is converted to give the by 0.72, then the Short also exceeded at the same
,
It is concluded that if cold venting were proposed as a normal operation then it would not be acceptable to BP or to environmental authorities. However, it is noted that the original design intentions were that the discharge would be of limited duration and of low probability. d) In assessing the safety implications of the discharge, the instantaneous level of HZS perceived is relevant. It is noted that the closest approximation of this is the 3 min average concentrations which shows that at elevated levels, and in particular the top of the amine contactor/regenerator concentrations in excess of 42 mg/m3 are predicted. towers, the HZS would cause eye and respiratory At these levels, tract irritation. This is unpleasant and would be a signal for evacuating the area. It is noted that if the 5 sec. average concentration (5 times the 3 min average concentrations in most cases) are considered, then levels in excess of 140 mg/m3 are predicted. These could cause a loss of the sense of smell and result in a loss of signal for evacuating from the However, the levels are below 700 mg/m3 affected areas. which would cause a loss of consciousness within 15 mins of exposure. It should also be noted that such duration for exposures are unlikely as explained in b) above. ' It must be noted that the effects of H2S depends on a number of variables and above limits are only for guidance. It is noted that people who are regularly exposed to even very low concentrations eventually become unable to detect the gas by smell. e) The models used for the dispersion calculations lose their validity at distances less than 10 metres of the In this area, it is also noted that the mechanism source. for dispersion is different and low flow emissions have greater impact on the resultant ground level concentrations especially if the gaseous emissions are denser than air as Within this 10 meter area of the in this particular case. Gathering Centre is the location of the pig receivers and wax traps which may well be manned in event of the cold vent operating. _ f) Analysis of the results given in Tables 2 - 10 shows that the dilutions resulting from cold vent dispersion increase as the flow of the emission decrease (see Fig 3) but is generally less affected by the concentration of the Low flOW6 would result during pollutant in the emissions. plant startup when plant upsets generally arise and
6
reduction of H2S content in using less sour wells would venting during this period.
the gas header by starting reduce the impact of cold
up
The concentrations of the hydrocarbons at the various g) receptors after dispersion has not been calculated; this be roughly estimated from the dilutions imparted on the pollutant during dispersion. Estimated hydrocarbon concentration for two receptors ha6 been calculated for Original Design Case 1 and shown below. Amine contactor, maximum H2S concentration is i) which corresponds to a dilution of 249. Therefore, concentration of hydrocarbon is 0.40 %.
50.7
ii) Incinerator, which corresponds concentration of
mg/m3 max
maximum H2S concentration to a dilution of 6636. hydrocarbon is 0.02 %.
is 1.9 Therefore,
mg/m3 max
It will be seen that in both case6 the concentration6 predicted are below the Lower Flammability Level assumed (methane) for this purpose.
7
can
2 %
5 OPRRATING
’i P
RXPERIENCE
During commissioning of problems were experienced discs which ruptured at have been due to fatigue HP/relief header. This from the burner and the composite material which
the Welton Gathering Centre plant with the use of graphite burst& low bursting pressure. These may caused by pulsation of gases in the was resolved by reducing pulsation installation of a bursting disc of has proved reliable.
After commissioning, the cold vent ha6 operated several times mainly as a result of instrument failure on the However the production through the plant was incinerator. below 50 % of the full capacity. With the recent modification6 to the incinerator, it has been possible to increase the flow through the Gathering Centre. This increase has resulted in the header pressures being close to the bursting disc pressure. This could increase the frequency of operation of the cold vent resulting from surge6 through the plant. If the existing incinerator is replaced by a new incinerator in the next Phase of the Welton Upgrading then the design of the incinerator and the setting of the bursting disc should be such that frequency of rupture due to surges is' eliminated.
6 CONCLUSIONS
AND RECOHWQiDATIONS
a) The study has concentrated on the dispersion of HZS based on a number of the Original Design and the Welton Upgrading gas compositions. It has been predicted that emissions would be odorous at ground level at short and long distances from the cold vent. b) At elevated areas, for example, the top of the amine contactor/regenerator towers, the predicted levels of HZS are higher than the Short Term Exposure limit. It is therefore recommended that access to the elevated areas close to the cold vent be restricted. Adequate warnings should be displayed at access points of the elevated areas and DA sets must be immediately available. c) The cold vent is located close to the incinerator and the pig receiving areas. These areas are likely to- be manned during operation of the cold vent. An audible alarm which is activated from a bursting disc failure has.therefore been installed to provide warning to personnel. Regular testing should establish that this alarm, located near incinerator control panel, provides adequate alarm near the pig I receiving area.
1’1 r1L
d) The plant licence was based on utilising the cold vent on The result6 of this study show that failure of incinerator. the emissions would be odorous and high concentrations of HZS are predicted at elevated areas'near the cold vent. It is therefore important that if operations are changed such that the design intention of utilising the cold vent is changed, then appropriate BP,authorities should be consulted. e) Due to the higher GOR's and plant surges, it is possible that increased pressures close to the bursting disc pressures are experienced as a result of the higher gas flows. This would increase the frequency of operation of the cold vent and represents a further constraint to the maximum allowable plant throughput. a number of options for. f) For the Welton Upgrading work, provision of additional gas disposal capacity are being Due to the potential hazardous nature of the investigated. it is recommended that preference cold vent emissions, should be given to solutions which remove the need to use a Such a route is provided if a ground flare is cold vent. selected to burnbgases on incinerator failure.
9
/i
g) In view of the complex nature of the safety and health hazard of HZS, it is recommended that an interpretation of - the GES dispersion results reported here should be obtained Any changes perceived from the original from HTH, Dyce. intentions of the using the cold vent should be similarly addressed. s c.t.
J. Caven-Atack A.A. Croll M. Broadribb J.A. Lewis E.A. Mullin/R.W. 1058/97
Bride=
10
iij ..--.
z ..~
un , O’I’U - --1--1- ..
..----w-v.-----,.YnJ -._ -.---.w(DLI11111, nn, Iall1 I nnn -----_ nllnpl ---.---.-.--_._
Nl
. WI, IuwaIY, IU n - --“U I’( (Iv.,** r A-_. nil onwt 0 .-. . . I-. -,
n3naMddv
I
I ISSUE *ROJECl
SCAlE
IO-q-t-Be PaoPo sc0 wb
h4
tlESCRIPIlON
DRN.
TITLE w
bxuoba
UC-Jr
=ack
Pr;loak
(WPS)
f-s
@ Kaldair
= &Do/ f*D. = s* sort+”
sficy
Q-1
OATE
0-n
Limited
DflG. No. E
-c
A CKD.
ENC.
:“N”t’
Figure
I
3
----.
I
‘n
*
2 0 t ‘A > [
,--
(swosnou) SZH
~0
stdounila
-- .-
r-
TOTAL
PROCESS ENGlNEERlNG DESIGN MANUAL
TEP/DP/EXP/SUR
. .
10,
?IPES VALVES + FITTINGS
Revision
:
Date
:
PageNo:
2/8 4
TOl”Ah
_ PROCESS PROCESS
OESIGN
ENGINEERING
AND
UTILITY
LINE
MANUAL
SXZING
TEP/DP/EXP/SUR
1. APPLICABILITY .
For a feasibility
.
For a pre-project
.
The purpose
.
For the both the fe’asibiiity
.
estimate
study a better
of the line size will be required. <
estimate
of the line size will be required.
of this guide is to size only the lines and pre-project
in the process unit.
studies
abaques
AFTP
can be used :
.
“Pour
le calcul
des pertes
de charges
des liquides
.
“Pour
le calcul
des pertes
de charges
des gaz dans les conduites”
The line sizing
depends
on the service
.
pipeline
and riser sizing
Flare
2. LIQUID
3. VAPOR
SIZING
FLOW
V2 criteria
are not included
on this chapter.
CRITERIA
LINES
SIZING
LINE
SIZING
CRITERIA
a stated
CRITERIA
for vapor lines to be followed
PP= m= =
:
2.
4. TWO PHASE
w
dans les conduites”
1. AND STEAM
See Table
P
lines,
LINES
See Table
The
study a quick
W WI, WV P’ F WI + WV = total
in kg/m3
flow rate in kg/hr
WI =
liquid
WV =
vapor flow rate in kg/hr
flow rate in kg/hr
W
and V = Vm = m.v f 0i = internal
diameter
with :
pl
=
liquid
density
in kg/m3
P’
=
vapor density
in kg/m3
m/s
$3600 4. of the line
om and Vm are respectively
in m. . the apparent
density
and velocity
of the fluid.
io :
I
-1 ,’
r~uc;tss
IUIHL
PROCESS
TEP/DP/EXP/SUR
.
AND
DESlGN
UTILITY
MANUAL
LINE
Revision
:
0
Page No
SIZING
I Date
The flow regime for vertical
.
tNWNEERING
to be checked
on the figure
1 for horizontal
lines and on the figure
lines.
For horizontal
lines slug and plug flow regimes
should
be avoided. l
.
For vertical
lines slug flow regime
Remark
: Flow chart
5. PRESSURE
DROP
5.1.
1 and 2 are based on author’s
FLUID
experimental
results.
“ABAQUES
(GAS OR LIQUID)
AFTP”
could
such as indicated 5.1.2.
be avoided.
CALCULATIONS
MONOPHASIS 5.1.1.
Fig.
should
Method
the correction
of the line
diameter
on these ABAQUES.
using MOODY
a. Calculate
be used with
or “regular”
Reynolds
Fanning
friction
factors.
number
Re = @i,Pv = 0i P v
=
r”, line internal
diameter
=
fluid
in kg/m3
=
velocity
density
in mm
the.relative
c.
f = friction
Determine
TWO PHASE Many
T
correlations
exist
of the vertical
temperature
conditions.
roughness
factor
in Cpo number
:
:
See Figure
34
E = D
See Figure
4 -+
f =
2
PV 2gx10.2=
:
to
f v 4%
bar/100
calculate
the
or horizontal
line,
m
pressure ratio
.
for
of vapor/liquid
two
phases
and pressure
BEGGS/BRILL
LOCKHART/MARTINELLE methods
drop
That is out of scope of this guide and we mention FLANIGAN POETTMAN/CARPENTER EATON
quick
viscosity
FLUID
depending authors
dynamic
Re is a dimensionless
i
5.2.
fluid
in m/s
b. Determine
d. ,.P=fxlOCx
=
Pe
for an estimation
are as follows
TAITEL/DUCKLER :
flow, anc
only some
2
TOTAL
PRO&S
I
TEPIDP/EXf’/SUR
X2.1.
PROCESS
“ABAQUE
LINE
AFTP” Takin
for
gas
as defined
using MOODY
Method
It is the same and the fluid
5.2-j.
MANUAL
A more section
be used
fanning
as on 5 5.1.2.
viscosity
taken
method
withy
the
Date
:
the
Page IJo :
0
=pm
10.3
2/8
correction
viscosity
friction
as the liquid using
:
with
in 5 4 and the liquid
or “regular”
method
detailed
could
‘Revision
SIZING
I
diameter. 5.2.2.
-:,L,-.R ,.1p., p,\?t . AND UTILITY
ENGINEERiN’C&SIGN
of
as the fluid
factors.
the
1
lir
viscosity
’
and V = Vm as defined
on g
viscosity.
Lockhart
cvartinelli
method
is g iven
i
I1 .O PIPELINES.
6. NOTES .
Tubes dimensions
.
With
are standard
“ABAQUE
estimation
AFTP”
=
the correction
of the line thickness
high pressure.
e
and an example
could
for
is given the internal
3.
diametar
be done with the following
must formula
be done and a used mainly
fc
’
thickness
mm
Y
bar g
0e =
external
bar
c
corrosion
P
=
Design
s
=
allowable
E
=
longitudial
5, E and
on Table
pressure stress weld joint
Y are not
= =
coefficient
having
values
diameter
for ferritic
steels
inch
allowance
mm
factor
always
available
so the following
formular
could
be used for
7
estimation. e=
P&f K
e
=
thickness
P
=
design
+c
in mm pressure
in bar g
c
=
corrosion
K
=
43 for carbon
carbon 0e =
external
For smail .
For
diameter
diameters
in inch
upto about
A P do not forget
allowance steel
in mm and low temperature
steel
54 for 3.5 % Ni and stainless 10” use the thickness
to take into
account
steel
given by the schedule
the change
in elevation
on Table
for liquid
3.
and tw
phase flow.
L
” TOTAL I’ I
1 PROCESS
ENGINEERING DESIGN PMICESS LINE
TEP/DP/EXP/SUR
MANUAL
Revision :
AND UTILITY
0
Page
:
NO
I
I
SIZING Date
1
: 2/05
10.4 -
-------------------_----
.-
.
--------m-m-
Y) --------
ir 00. -4.
*Q) -II.
.
22
?- . aa
m c;
00 Y-
------------
-I:
VI
22
.*a
?00 c-
33-------q
.
! ,
-
-1: / -
.-
?-rr\
.
Ov\ . -rr\
.
wo . 3m
.
v\ 4
wo $6
,-
---------
-----------------------
-
E 2 3; -
TABLE
I I
1 VAPpR
AND
STEAM
LINES
1 VAPOR
LINES
.
. .
I
.
P < 20 20
80
V2
1 Pv=ysd;:;;:it;$;3J
/
/
MAXIMUM
2
bar g < 50 bar g < 80 bar g bar g
I I .
6 000 7 500 10 000 I5 000
, I
I -
I I
Discontinuous anti-surge I
operation . - P < 50 . 50 < P . P > 80
eg: compressor b& g < 80 bar g bar g
I
:
, STEAM
I I -
P
. .
1
I
I
I 1
Short line L < 200 m Long line L > 200 m
I I I II
.ShortlineL<200m * Long line L > 200 m
I I I
i T;ore a
LINES
vELz;lTy
I
I
A P bar/km NORMAL
;
MAXI
I AP
must
,1
I
be considered
I 1
I IO 000 15 000 25 000
I
i
1 i and be compatible
with
, ) the corresponding
service
f
,
suction discharge
MAXIMUM
, )
I compressor compressor
I ,
I
I
I
’
compatible
with
0.25 0.5
0.5 0.15
I
1.0 0.25
42 42
1.2 0.25
I
2.3 1.0
30 30
1.2 0.35
!
“2.3 1.0
.
f -
lO
/ ,’ - P > 30 bar g
. .
Short line L < 200 m Long line L > 200 m I
I I
I
I
I
‘TOTAL
PROCESS ENGINEERING DESIGN MANUAL
/ Revision
:
0
Page NO
PROCESSANDUTILKYLINESIZING
TEP/DP/EXP/SUR
Date
: 2185
10.6
/ :/
7. REFERENCESANDUSEFULLITERATURE . .
LUDWIG
.
Flow of fluids
.
“Gas liquid
l -
CRANE
flow in pipelines
Pup1 by A.G.A., .
“Gas liquid
flow in pipeline published
.
“Proposed
correlation
pipelines”
LOCKHART,
BEGCS
, H.D.,
TULSA .
ABAQUES
II - Design
manual”
C.O. COLDREN, by A.G.A. of
by A.E. DUKLER
by 0. BAKER,
FLANIGAN
May 1969
H.W.
and J.K.
WELCHEN,
October
data
for
isothermal
J.P.
Manual
“Pour
le calcul a conduites”
.
“Pour
le
two
MARTINELLI
.
for “Two
des
two
component
flow
phase flow in pipes”
penes
de charges de
1975 university
I I
.
“CHEMICAL
PROCESS
dans
les
des
dans
les
charges
gaz
W. WAYNE
BLACKWEIL,
.
I I I
I
“Two
PROGRAM
phase pressure
DESIGN
ON A PROCRA.MMABLE
CALCULATOR”
B.S. Page 22
drop computed”
- Mafik
Soliman,
of
des liquides
I* PEPITE
in
(1949)
des pertes
calcul
phase,
conduites” .
1970,
and API
R.W. and R.C.
and BRILL, I
AFTP:
results”
HOUSTON
API and Union’of
BRAINERD,
.
I Research
Hyd. Processing
April
84
I7
TEP/DP/EXP/SUR
TE
8Ucer. rt81k NW. 0.
OII nd
10. 1956,
Jourp. 156.)
Gas
: ) i I
.. I I I I 1 /
0.4 Q6Od LO
! .A i
2 0x
OSHINOWO FOR
- CHARLES VERTICAL
TWO PHASE FLOW UPWARO FLOW
MAP -
FIGURE
2
00.0 Qs - Vapor flow rate. Ft3 /See flow rate. Ff3 /See Gl - Liquid . 0 - Pipe inside diameter. inches p 1-
i
I
I 1.0
Liquid
u 1 -Liquid p 1: Liquid
densicy.
Lh/Ft
-
.
3
surfra tension, dyne/cm viscosity centipoiro
I I I I illli
II I I111111 I ’ BUBBLE QUIET SLUG OISFERSEO SLUG FROTHY SLUG FROTH ANNULAR
40:
(
7
f .
TOTAL 1 ,
TEP/DP/EXP/SUR
-f
PROCESS
ENGINEERING
-
MANUAL
Hevtslon
:
0
I
I
SIZING
3 - Relative
Date
roughness
: ,
’ : 2185
of pipe .
..
Pipe Diameter. in Feet -D
bIJ6 pa3s g .mo4 z .aa a
.oalos .CCICJO~ .umi .aJaM
.ooGQo6t
1
Page
No
PRDCESS AND UTILITY
Figure IOUfi6.)
DEStGN
11
1lllllll I I
I I Ill”” DOOOOS~ 3 2 1
III
4 56
I
I
8 10 Pipe Dtamekr,
to in
30 40X160 Inches - d
EOlOO
I,,
200 300
10 -0
:
“y’?-“$q,.
Revision : f, TEPIDPIEiPISUR ,
L=
SXZXNG
FRICTION FACTORS FOR CYLINDRICAL PI PE
Date
O
: 2/85
II
Page No :
10.9
‘I- TOTAL
1
(1
ENCilNtttilNlA
PROCESS
I
TEP/DP/EXP/SUR I-
PEbocEsS LINE
IJtblCiN
A?lD UTILITY
NBE NORKAL
. s’
17. I4
1.:)
I
f
II.%
2.11
i
.. ,,a-
a2.16
2.77
I Ill-
l .26
I
SO.JI
21'
71.0?
Notes
THICKNESS
I
2.77
;
r.u
2.77
1.U
LO1
1.77
J.91
s.n
J.14
7.01
1) 2) 3)
For me For
schedule follovrnq
00 >
I
3.71 I
3.n
”
rage
Date
: 2/h
I
IN :w
1
1 I
!
_i
!
1.1 I
s.m
1
I
X.77
3.3)
j
Las
I.%
l .a>
*.70
7.M
Au
>.0t
IO.10
1.71
J.9?
5.n
II.07
V.J2
&lb
?.OI
lb.01
1 b.?S
I
_ i I I
10 0 < 14' 4re nor used normally diameters are not common : l/8', 3/a-. 30' line drametcrs increase in 2‘ incrcmnts
NO
:
I
-iW.
mom 1
.
I.1
DIXENSIONS
TOLERANCE
2.11 1
3.06
:
WI-I-Ii
I
SIZING
TABLE I
nc.,o~“II
MHNUHL
I l/4-,
i
2 l/2-,
1.0
3 112',5-
IO. 10
4 :
TOTAL
PROCESS
:
,~,
v.
.
ENGINEERING
MANUAL
0
Revision
:
Date
. Z/85 .
Page No :
’
CLASS
TEP/DP/EXP/SUR
I.
_ 1
DESIGN
PIPING
(._
_,,
,,
10.11
,
APPLICABILITY The purpose when
the
feasibility
of this
piping
chapter
material
is to determine class
and pre-project
the piping
document
does not
class used as shcwn
exist.
This
on a PID line
is generally
the
case
studies.
2. CLASS
NUMB&RING
PRINCIPLES
(From
2.1.
GENERATION
OF NU,MBER
DD-SP-TCS-
112 “PIPING
MATERIALS
for , ,I
CLASSES”)
‘
1
I The class number two-digit
number
material
used
shall
consist
of a capital
representing for
the
the main
valve
bodies,
letter
material tubes,
representing entering
fittings
the ANSI
into
series
the composition
and flanges
of the
and 3 of
network
* in
I.
question. I Example
: Ear . . l
Series The
tables
below
.
: . . . . . . . . . . . . Carbon
150 . . . . . . . . . . . l
give
the
I
letters
steel
and numbers
to be used
for
numbering
classes. 2.2.
LETTERS
representing
the series of the class
Series
I 125 I 150 I 250 I 300 I 400 I 600 I 900 I1500 I
Symbol
2.3.
I
I
I
I I
I
2500 I
Trying I
I
lA~BlC;D~EiFtCIH~J~
NUMBERS
representing
Y
the main
oito20
:
Carbon
21 to 45
:
Alloy
46 to 70
:
Stainless
71 to85
:
Special
alloys
86 to 99
:
Other
materials
material
steels (ordinary,
of the class
galvanized,
normalized,
steels steels (Monel,
Hastelloy,
(Cast-iron,
etc...)
copper,
Glass Plastic,
etc...)
cement-asbestos
fiber,
etc...
copper
alloy,
etc...)
piping
PIPING CLASS
TEP/DP/EXP/SUR
3. PRESSURE
Date
TEMPERATUREi
The following STANDARD For pressure
ANNEX STiEL
PIPE
temperature mainly
10000 PSI, . . . (used
: 2/85
10.12
RATINGS C is extracted FLANGES ratings
from
ANSI
B 16-5
AND FLANGED higher
than
for well tubing
1977 (AMERICAN
NATIONAL
FITTINGS).
series
2500 the following
is used 5000 PSI,
and wellhead).
I nd a FIG.
kin
4
Prasruro-tcmperoturc
ratings
for
steel
flonger
C ond
flanged
fittings
from
ANSI
B16.5-
1977
’
.28.9
to 37 B
-20
to 100
275
027
E
E
ra2
900
so
538
950 loo0
::
“3U
649 704 760 851 NOTES.
1200 1250 1300 t:g 1450 15W
--_ E 375 325
195 155 ‘A2
525 520 510 iii
z: 14s 110
E
“62
5-z
::
45 30
::
1% 105 70
310 240 170 120
515 400 205 200
-4 I
I
ToT’AL’
PROdESS
ENGINEERING
DESIGN
I
MANUAL
Revision
:
0
Page No :
, I
SELECTION
OF TYPES
OF VALVES
TEP/DP/EXP/SUR
Date
:
Z/85
10.13 1’ ! 1
1. APPLICABILITY
I’
The purpose
of this chapter
is to determine
the types of valves
used for designation
PID. .
on tht
t valves
are used for two mains
functions,
isolation
1’
and control. I
The following piping 2.
is only
material
BLOCK
a guide
line
class document
for
selection
of types
of valves
which
must
follow
thf
when it exists.
I
VALVES I
The main
2.1.
types are :
BALL
ball
.
Plug
. .
gate butterfly
I ’
VALVE
Ball valves I 2.1.1.
.
Full .
can be full bore or reduced
I
bore.
bore uses flare
I
system
: upstream
and downstream
of PSV, rupture
disc, flare
line
if I
required.
2.1.2.
.
downstream
.
vents and drains
.
piping
.
for block
.
utility
2.2.
PLUG Plug
and upstream
on’hydrocarbon
valves on instruments valves
except
Reduced .
pig launcher
lines if the pressure
for diameter
on hydrocarbon
service
VALVE USES . valves have the same use as reduced
are smaller
I
for hydrocarbon.
larger
drop is critical.
than 2”.
bore uses
Block
(600 * 1. Plug
I I
equipments.
an hydrocarbon
water
pig receiver.
valves
can be assimilated
and lighter
of the two.
without
solid particles.
I
I bore ball valves when used for high pressure to reduced
ball valves,
generally,
plug valves,
I
I
0:
I
t’HUCkSS
TOTAL
SELECTION
TEP/DP/EXP/SUR
I’
t3.
tNtiINtERING
GATE
VALVE
DESIGN
OF TYPES
Revision
:
Date
: 2l8S
MANUAL
OF VALVES
0
Page NO :
10.14
USES
I tht
l
I’
.
Gate
valves
upstream greater
2.4.
can be used as ball valves
of pig receivers.
The vertical
for downstream of pig launcher ant a physical space required by a gate vdve is
than a ball valve.
.
Tight
.
For hydrocarbon heads.
service
.
For quick
closure
purposes.
.
On utility
lines for low diameters
shut off for ball or plug valves is superior
BUTTERFLY .
except
VALVE
On water
lines
with
solid
to that of a gate.
particles
presentor
as wing
valves
on well
< 2”
USES for service,
utility
or sea water,
generally
for diameters
larger
than 2”. I 3. CONTROL e if
I
VALVES
,
The .main types are :. .
3.1.
GLOBE .
3.2,
3.3.
VALVE
Control
globe
.
butterfly
.
special USED
valve
used in most
instrument
group,
throttling
purposes.
BUTTERFLY
VALVE
.
On water
networks
.
Throttling
SPECIAL Special
valves
or on water
networks,
at very and
suction
USED
are defined
by instrument
.
for very high A P the angle valve could
.
for compreSsor
anti-surge
group
:
be used
cage valves could
high
compressor
USED
at compressor
VALVES
of cases except
be used.
P as defined suction
lines
by for
TOTAL
-ENGINEERING .’
PROCESS
A P THROUGH
DESIGN
VALVES
AND
MANUAL
Revision
:
Date
:
0
Page No :
FITTINGS
TEP/DP/EXP/SUR
2m
1. APPLICABILITY The purpose This
may
of this chapter be required
consideration.
For
is to calculate either
for
most
precisely
study
projects
phase
however
the pressure
for
drop in a piping
situations
calculation
A P is a critic line ‘- A Ps wil not
where
of process
required. The pressure 2.
drop calculations
A P THROUGH.
VALVES
2.1.
OPEN
VALVES I TYPE
are based on a summation
GATE VALVE
I
I !
PLUG COCK NALINE
5
f I
I
I =
K
2.2.
BALL
extract
I
density
in kg/m3
v
:
fluid
velocity
in m/s
with
reduced
bore : This
A P depends
BALL
VALVE
PRODUCTS
is given
on the valve
vendor.
as an example.
below
gives
in cylindrical
DE CHARGE
some
values
conduits.
by I.E. IDEL’CIK,
of
For
the pressure
further
drop
information,
EYROLLES
edition,
coefficient refer
K for
fit. ..,
to “MEMENTO
DE
PARIS”.
A P in kg/cm2
P v 3.1.
: :
fluid
density
in kg/m3
fluid
velocity
in m/s
AP=K
.@” 1.962x105
ELBOWS K values for elbows. I I R/D I f
90”
I ,
4s”
f
q
1
FITTINGS
example
PERTES
I
1 bar = 1.02 Kg/cm2
ball valve
of CAMERON
3. A P THROUGH
encountered
I 2.4
VALVE
A P through
The
i
.PV2 1.962x105
fluid
:
CHECK VALVE
0.1
A P in kg/cm2 P
1 I
0.15
A P
I,
I
K
1 I
GLOBE VALVE
I
K method.
friction
1 I,
1.5
0.17 + 2.36 f 0.11 + 1.18 f factor
see chapter
3
I 1 1
0.12 + 4.72 f 0.08 + 2.36 f
PROCESS/UTILITY
5
I
-LINE
f 1
0.09 + 7.87 f 0.06 + 3.94 f SI,ZING
§5
I I ;
I
TOTAL AP
'I%Rm-
VALVES
AND FITTINGS
Date
TEP/DP/EXP/SUR
: 2/85
10
20
30
40
60
loo
0.47 0.45 0.42 0.39 Of7 0.27
0.45 0.41 0.35 0.32 0.27 p.18
0.43 0.36 0.30 0.25 0.20 0.13
0.41 u.33 0.26 0.22 0.16 0.11
0.40 0.30 0.23 0.18 0.1s 0.12
0.42 0.35 0.30 0.27 0.25 0.23
I*0
lcl,ld
180
0.45
030
0.41 0.40 0.X 0.31 0.36
0.50 030 0,SO O.SO 030
TOTAL
PROCESS
ENGINEERING
A P THROUGH VALVES
DESIGN
MANUAL
Revision
:
0
Date
: 2/85
Pabe No :
AND FITTINGS 9
TEP/DP/EXP/SUR A
s, +5a > s,
T TE
10.17
I
’ ‘I
I
TOTAL I TEPIDPIEXPISUR
---
PROCESS
ENGINEERING
DESIGN
MANUAL
.i
TOTAL TEP/DP/EXP/SUR
PROCESS
ENGINEERING
DESIGN
Revision
MANUAL
:
0
* No : Page
AP THROUGHVJUVES AND FITTING.5
TE
I
I
Resistance’Coefficient, The
resistance
coefficient
is calculated
Date
K
by the
formula:
K-fL
0 Valves of the friction factor. f. for various pipe sizes are listed in table l-17. Values for L/D and C for fully opened valves were calculated from theoretical considerations. Valves of C. for partially open valves were extrapolared from ten result for representative sizes of ball valves. Chart 1 * 18 provides graphic represenration of valve position versus the percent of full open area.
Table I-17 Friction Factor (r] tw-ald hoesa ;
.6' c 1r lz1‘. 16' :c 22-
Calculated Cameron
hcla FUl~(f-l 0190 017s 0164 OISO 0140 013s 0110 0125 0123 .-0110 . 0117 0116
FrLprn Fanor tn
I-I *DCslrc 14’ . 1 :: lo34. 36' UT I
z
_- . '.
)
0115 0113 0112 .OllO .' 0107 010s 0104 0103 0!02
!
.
L
Table I-3 Values of L/D for Full Opening Ball Valves in Full Open Position
: 2/8s
I
10 -19
pflUl;tS
TOTAL
CNbINCCnINla
..“.,~,“,I .v UCSIWY IVI~IUUAC.
l
Date
: 2/8-s
10 -20
Table l-5 Calculated Values of L/D for Reduced Opening Cameron Ball Valves in Full Open Position l
‘I
Table I-6 Calculokd Values of L/D for Venturi Opening Cameron Ball Valves in Full Open Position I
I
I
a.”
AP T’HROUQI VALVES Brad FITpINc;s
TEP/DP/EXP/SUR
I
“3”
I
.
f
t
TOTAL
.
PROCESS
ENGINEERING CONTROL
DESIGN VALVE
Revision
MANUAL
:
0
PageNo:
l
1 !
SIZING
:
Date
TEP/DP/EXP/SUR
Z/85
10.21
,,
1. APPLICABILITY The purpose control
of this chapter
valves
installed
for one
valves in case of revamping. 2. CONTROL These
VALVES
2.1.
given
service,
The final
principally
available
QUICK
formulae
some
the size and the number
to estimate
and
sizing
to estimate
should
the capability
be done by instrument
o- ’
of the contra
,
people.
.
.i
CHARACTERISTICS
are determined
characteristics
is to give
by the
are quick
design
opening,
of the valve
trim.
and equal
percentage.
linear,
The three
fundamental
1 ;, L1
OPENING
As the name the seat
implies,
with
application
lesser
this type provides flow
if for simple
increase
on-off
a, large
opening
as the stem
control
as the plug is first
opens
further.
with no throttling
The
lifted
most
f roar
,
common
. .
of flow required.
2.2. Linear
trim
provides
plug position 2.3.
EQUAL
equal
.
.
provide
increase
in rate
of flow
a very small
toward
the
fully
practice
at maximum
flow is smalier
than or ‘equal
For normal
flow
opening
the. valve
if applicable,
for
opening open
equal
increments
for plug travel
position.
of stem
I .
near the seat
As a result,
a wid
the opening than
to select
a valve in which
I’
the valve openini
to 95 per cent.
should
be at least
should
be larger
than
10 per cent,
a smaller
valve
60 per
LO per cent. should
while
cent
for
minimum
If the minimum
be installed
fl
in parallel
I : iS; ,
wit
i
valve.
For a flow rate vendor
witr I *
increases
only it is common
close to or smaller .
is linear
RANGEABILITY
For an estimation
the ‘main
Thus the flow rate
of flow rate is achieved.
VALVE
flow,
travel.
.
percentage
large
rangeability 3. CONTROL
in stem
its travel.
The characteristics very
and
throughout
increases
PERCENTAGE
Provides travel.
equal
in their
the valve
opening
depends
on the valve
characteristics
and
1 1
it is given b
catalogue.
.. 1~
4. FORMULAE The valve
area is characterized
by the
coefficient
Cv (except
for FISHER
which use Cg for1
the gas (see hereafter). The
Cv coefficient
through
a restriction
The following corrections the formulae
formulae
is the number and
the pressure are simplified
may be necessary given
of U.S.
gallons
drop through and
in their
flowing
this restriction
to be used
for the installation
by manufacturers
of water
equal
during
one minut
1 PSI.
only for an estimation
of reducers
around
car-logues
will
of the Cv. Sam, e the control valve. If so‘7
be
used
for
a better
C-V
Calculation.
i
“.-
TOTAL
PROCESS
,.
-
ENGINEERING dONTROL
DESIGN
VALVE
:
0 .
Date
:2/u
Page NO :
SIZING 1.
TEPIDP/EXP/SUR 4.1.
Ravision
MANUAL
10.27
LIQUID I
A - Sub critical
, i
tntak
flow
I
Pv
-PZ
Cv = 1.16 Q
sg PI - P2
J
Ps
B - Critical
I bl I I
flow
-PZ>Cf<.*Ps I 1.16 Q J CC
sg
A Ps
L bI roll-
,
motj
;
Cf
=
critical
flow coefficient
(given
type of valve and the action
I’L a uitt
Pv
=
fluid
PI
=
upstream
P2
=
downstream
vapor pressure pressure
by manufacturers
of valve
by increase
and
of variable)
in bar in bar
pressure
in bar
APS = Pl - (0.96 - 0.28 1 C)Pv
ring
I
. .
lum I : iY’ ,
4.2.
or to simplify,
if Pv < 0.5 Pl,
PC
=
fluid
critical
Q
=
flow rate in m3/hr
sg
=
specific
APS = Pl - Pv
pressure
gravity
in bar
at upstream
at flowing
conditions
temp.
(water
= 1 at 15°C)
GAS AND STEAM I
A - Sub critical PI - P2<0.SCr2Pl
flow
I I I
0 - Critical PI-P2>,0JCf2Pl
flow
depends
on tf cf < 1
I
TOTAL
PROCESS
ENGINEERING CONTROt
DESIGN VALVE
MAhiUAL
Revision
:
Dare
:
0
SIUNC
TEP/DP/EXP/SUR
SATURATED
2/u
STEAM I
72.4 W
cv = J (Pl
- P2) (PI
+ P2)
I
I
.
SUPER
HEATED STEA&M I 83.7 (1 + 0.00126 cv _ 72.4 (1 + 0.00126 Tos) W i cv= Cf PI &PI - P2) (PI + P2) f Cg, PI,
4.3.
P2, Q same definition
=
relative
T z
= =
upstream
gas temperature
upstream
compressibility
W
=
steam weight
Tos
=
steam
TWO PHASE
density
and unit as 5 4.1.
G
(air = 1.0) OK = 273 + “C factor
in t/hr
superheat
in “C
FLOW
For sizing,
maximum
A - Without
liquid
A
P = P 1 - P2 = 0.5 Cf2 P 1
vaporization
I I
B - With
JP
(dl + d2)
J
Cg, PI, P2 same definition w
=
total
dl
=
upstream
fluid
and unit
as 5 4.1.
flow in t/hr mixture
density
in kg/m3
w x 103
d=
EL+
dll
Wlv dlv
WI1 =
upstream
dll
upstream liquid
density
Wlv =
upstream
vapor
flow in kg/hr
dlv
upstream
vapor density
= =
liquid 36.6 W
51.8 W
cv =
liquid
flow in kg/hr
--
Page No : c
in kg/m3 in kg/m3
APdl
vaporlzatlon
Tos) W
1 O-23
PHUCtSS
“1 UTAL
tNbINtERING
A P THROUGH
TEP/DP/EXP/SUR
DESIGN
VALVES
AND
MANUAL
Revision :
d2 =
4.4.
FISHER
density
: 2/85
in kg/m3
w x 103 w21 w2v -+d21 d2v
. It
w21 =
downstream
liquid
flow in kgjhr
d21 =
downstream
liquid
density
W2v =
downstream
vapor flow in -kg/hr
d2v =
downstream
vapor density
in kg/m3 in kg/m3
FORMULAE
For gas “FISHER” cv=
mixture
use Cg instead
of Cv
cg Cl Cl = valve coefficient
(given
by catalogue)
fw
./T]
cg = 0.4583
d PI sin
deg.
w = gas flow rate in kg/hr d
5.0.
=
gas density
Pl =
upstream
P2 =
downstream
REFERENCES
at upstream pressure
AND USEFUL
-
Vendors
documentations
-
GPSA chapter
2
conditions
in bar also
pressure
Page
NO
FITTINGS ,Date
d2 G downstream
O
in bar also
LITERATURE
in kg/m3
10.24
:
--
TOTAL
PROCESS
ENGfNEERlNG
DESIGN
MANUAL
TEP/DP/EXP/SUR ,
. +-
11,
I
-/
PIPELINES
Revision
:
Date
:
Page No : Z/85
.
TOTAL
Revision
:
0
Oate :
2/85
Page No.
PIPELINES
TEP/DP/EXPlSUR
11.1
L
1. APPLICABILITY For
both
feasibility
and preproject
long pipeline
be performed
estimate
by hand. Details are given below on how to proceed on this.
2.1.
PRESSURE
or RESEAU-
A P and AT calculations
normally
2. PIPELINE
using PETITE
studies,
It may be necessary,however
to make an
DROP FORMULAE
GAS TRANSMISSION There exist many methods of calculating American
are :
AP for gas transmission
Gas Association
lines. Some osf these
Formula
Weymouth
Panhandle ‘.4’ and ‘0’
Darcy
Colebrook Below is given the Panhandle ‘A’ for use : 1.8539 CO.4604 X x 1 2.6182 E; d X 1 Where
TS
ps
T Lm
‘-2
q d z E
The formula does not take into account significant, can be added to the A P calculated LIQUID
TxL
x
m
= Upstream pressure = Downstream pressure = Specific gravity of gas = Base temperature = Base pressure = Gas flowing temp = Pipeline length = Flowrate at Ts, Ps base = PIPELINE DIAMETER = Average gas compressibility = Efficiency (0.92 for a clean line)
Pl P2 G
2.2.
will
5
x 0.301s
bar (a) bar (a) K (271 K or 298 K) bara(1.01325 bar) K km m3/d (at Ts, Ps) cm
the pipeline if required.
profile
which,
if
FLOW IN PIPELINES
Use Darcy equation
:
P = 6.254
F
,M2
P
D5 kg/h
F
=
Moody friction
Density
kg/m3
E
=
Absolute
=
line id
cm
=
pressure drop
b.r!km
=
Mass
= D CP
flow
bar/km
factor
roughness
cm
(see page 10-S and 10.9) =
viscosity
CP
TEP
Revision :
TOTAL
0
Page No. :
PIPELINES Date :
TEPIDPIEXPISUR
vi11
2/8S
11.2
.
an
Re =
35.368
M
x
x D with
:
A = 2.457 [
F
= 64/Re
F
= (S/Re)lZ [
Ln
BE
l
2.3.
3/z 16
+ (0.27
1
E/D)
1
“I2
*iOr Re > 2000
using
friction
factor
F and FANNING
F”
:
charts
as confusion
arises
F’ = l/4 F
HORIZONTAL
Estimating
2-phase
the flow
characteristics
estimate
when
MOODY
TWO PHASE
2030
(37530/Re)l6
CAREFUL
between
<
+ l/(A+B) 1 -------
(7/Re)-9 B=
for Re
flow
A
P by hand for long pipelines
and equilibrium
will
A P can be hand calculated
of
alter
along
providing
is not recommended,
as
its length.
an
the phase
However
regime
is fairly
stable. Given
below
BAKER
is
a calculation
method.
or process
This
method
method
based
can be used
on LOCKHEAKT-MARTINELLI-
for both
longpipelines
lines.
METHOD , *’
AP
2 PHASE
1. Evaluate
OP
=
flow
regime
and adjust
2.
Calculate
APC
3.
Calculate
APL
4.
Calculate
5.
Calculate
AP
6.
Calculate
APvert factor
For convenience
( APL/A
HORIZ
factor.... (vertical
pipe ids are in cm
.(-.
AP
Pipeline
VERT
0 if required
PC)“’
2 PHASE
viscosity
+
is in cp.
Pz H section
of pipe)
(stable
regime)
. r
11.3
OPERATING
I
I-l I I I I-
DATA LIQUID
FLOWRATE DENSITY VISCOSITY
FL0
WING
PIPELINE INTERNAL
Wg Dg “is
= IOQOO3 = 1E = O.Ol’LA
kg/h kg/m3 CP
TEMP DIAMETER AREA
D A
“C
= 3L
cm m2
= .b.cI, = 2.13
FL0 WRATE DENSITY VISCOSITY SURF TEN
WI kg/h 01 kg/m3 Vl cp St dynes/cm
= :;o 3co zp 1 So J f r i:
I /
jPIPELINE Vertical
LENGTH change
L
A h
m m
= 103J = - :LO o
I( I I / I-
STEP ;
I.
DETERMINE
6x
=
I
FLOW
210.3
.!!!
REGIME /Dxi
’
I
BY =
2.
FROM
BAKER
Re =
St
= 3ci.63
I
I I
I I
CHART
I
3;s7c:;f
ire P”JCIO.7 i
L
Apgas
CALCULATE
I I
1
x VII/~
7.087 x w Ax DlxDg r -7----F
REGIME
I
I
t
D12/3
wg
NOTES
I
35.368 x Wg Vg x D
1 Fricilon
factor
(:vloody)
I
I APL
6.254
x f x Wg2 Dg x DJ
s;
1 1
3.
ApLIQ
CALCULATE
I I
Re=
1
APL=6.254xfxw12
I
35.368 x WI VI x D
I I APL I
\-. DI x 05
PROCESS
TWO PHASE PVELINES A P CALCULATION
P’ooPmIP/EXP/SUR
I
I
CJiK
DATE
JOB
TlTLt
E LJ\V
I ii
;-
=-&ar/km
I
I
CALCULATION
SHEET
Sheet
I of 2 I
ITEM : NO. JOB
HO.
REV
1
I 1t -
LIY
‘ya I
-. c
3
1 I.4
. I I.
I I
4.
I
AVERAGE v, =
5. CALCULATE
) 6. CALCULATE ws =
I I 7.
I
II
I V, = :?- cc I I I
in/s
VELOCITY
I.
LOADING
FACTOR
WS
I
WI x 0.205 7
CALCULATE
PH FACTOR
FOR
) wsJ??,‘O
I
i
I
I
I
HORIZON-t-AL
FLOW
-TYPE
OF
FL&’
I
X RATIO
FLOW TYPE =&Pi C: .j I
PH
i
PH
BUBBLE
STRATIFIED
I :w
SLUG
------t-WAVE
I I+,.~. I IA Pa
:
rt vt pc , ,‘.tSt
-a-In FH + 01111 Ftl
VC=
IpcD’
lntix aul
-- LVVJ
FLOW
---
TYPE
= WAVE
f I
APa-,=
ht.-
t1
bar/km
‘I I I I
8.
CALCULATE
PH FACTOR
VERTICAL
i
FRN
.
SECTION
i
x0
.
0.19
V21D
(X)
VERTICAL
SECTION
Cm
Vinmh.Om
f
(FRNl”“”
n
PH,
=
I.510 I
x . x0 in oi~pcrvd fbr eq~. (0 SC’ Pn .w.
lI
t
IC.2
FOR
1 I
I 9.
CALCULATE
TOTAL
I
I I _.
Horizontal Vertical
I
TOTAL
: : &P
TWO PHASEAP
PH = I.888 PH,,= I.~\0
= (bp2H
x L +Apzv
AP2” aPzv x h)/lOOO
=
4,~~ =~PG
x PH2 x PH$ = q
1.5-i’
1.3AQ
o.?i?
bar/km bar/km
bar
I
I
I PROCESS
TWO PHASE PIPELINES P CALCULATION
TEP~OOP:DIP’EXP’SUR IY
f 1 1
CHK
1 DATL
JobTlTLt
TM\.+<
CALCULATION
SHEET
Sheet 2 of 2
ITEM NO I08
NO
REV
.
Revision :
TOTAL
Date:
TEMPERATURE
No.
and accurate
the program
PEPITE
11.7 is accurate to a small
2/85
Il.5
I
,
PROFILE
For detailed
segments
Page
PIPELINES
TEPIDPIEXPISUR
3.
0
AT
should
to within
programmable
AP calculations
and
in 2 phase lines buried,
be used. The hand calculation 10 % for both gas and liquid calculator
and increases
method lines.
presented
The procedure
in reliability
subsea or in air on pages I 1.6, is easily adapted
the greater
the number
( *b
of
used.
The following
D h
should be remembered
For long pipelines
assuming
when designing
isothermal
pipelines,
flow can result
in overdesign
in pipeline
i
-
sit
PI P2 . AP Tl
AP.
1
If the pipeline is constant with regard to material, insulation route a fixed thermal conductivity (k) can be assumed. For gas pipehnes
the internal
film
resistivity
is neghgible
and burial
depth
along
its
I---l
I
- ignore
II I
it.
.
1.
I I
For all steel pipelines
the
resistivity
of the metal
is also negligible.
j I
Small
pipelines
(< 20”) have a large
heat
flow
compared
to the specific
heat
of the
in a relatively
short
L
flowing
medium.
Consequently
length.
For large
pipelines
the gas will
the converse
reach ground/sea
temp
is true and a long distance
is required
j
to reach
For oil and small
gas pipelines
For large diameter
The attached versa,
calculation
the asymptotic
temperature
gas lines, Ta depends sheet
largely
Ta is that of the surrounding on the Joule-Thompson
can be used for hot lines
in cold
,
effect.
surroundings
or vice
’ :
-
I3.5 I
.
I I I-l 4. I
I For subsea pipelines, transfer
coeff
epoxy wrapped,
of U = IO - 15 kcal/hm2’C 6
concrete
coated
resting
is a good estimate
on the bed an overall for calculation
purposes.
heat b
2.
I I
‘
ambient
medium.
1
.
I I-i Re I Set IL TO. If
5-r-r
PcJDPfC
11.6 Covering
1 air ’ / ; 1.6, >ted ii
rOf
, *:
/ I
D h
/ *
PI I
. aF2 Tl
Total pipeline length No of segments Length per segment Total elevation change Pipeline diameter Pipeline diameter Burial depth to centre
m +m Ls m m
= ?3BOO =& = 1oeoe = 4 103 = 30 = o.-Gt = r-t>
Inlet pressure Exit pressure Total pipeline initial Temperature
bara bara bar ‘C
= = = =
m
FLUID JOULE THOMSON (see fig. I, page 11.8)
1
= rc “F/1000
psi ( I I I I I
VALUE I
I I 1.
Calculate
heat
transfer
factor
s
1 = 3.33
x = 2h/D s= 2kn /ln [ x + (x2 - 101
‘C 1
m3/d (std)= 00 O*CJ = 15 = -locJ;.s kg/h kcal/kg’C = 0.6 x 0.00805)
I NOTES Coverinq
~(&~ Y 0.f 17 -l-
k kcalThmC
I
i
I
I
I
I
I
I I
I
I
/:
I
= 5 kcal/hm’C
1
) 2. Calculate
heat flow ratio
leqth
I
a = s/MCp
‘,
I I 3. Calculate
(liquid
Asymptotic
per unit ‘a
or gas)
I a I I
=113-q ,o-c.n- 1
Ta =Tg - (1 AP + L\ y/jCp)/aL
1.49 0.022 0.508
.
I
0.30 1.49
I I
I I
I
temperatureTa
- ..*
f
i
I
1 Ta =41\ ‘C
i L is segment 1 j= 426.5
I
length w
I
kcal
I
1 I
I
I
I T2 =Li-k”c I
I I I I
I
I I
I I
I I
/
/ . I 4. Calculate
I downstream
ternp
I
-1-2
I I
T2 = (Tl
- Ta)e-aL
+ Ta
f . . I I Repeat steps 3 + 4 for each segment ) See sheet 2 for stepwise spreadsheet
I
.
PROCESS
/
/
BURIED
PIPELINE
AT
CHK
CALCULATION
CALCULATION
SHEET
I I
Sheet
1
of 2
---
ITEM NO.
TEP~DI~~I~IP,ExP~u~I Br
= C.L;“C/bar
I
I
-
= =
e
f Soil I Air I Water I Sand dry I Sand wet I
I
I
= I3 = I. /,q
GAS FLOW
I STEP
“C kcal/hm”C
.
Volumetric flow Molecular mass ,M Mass flowrate Cp Specific heat
I
I
FL0 W
Volumetric floum3/h Density (av) kg/m3 M Mass flow kg/h Cp Specific heat kcal/kg
A0 50 IO LB
COEFFICIENT
:
Temperature Therm. cond.
Tg k LIQUID
Medium
OATL
I JO8
TJrLf
;-%AflPl
C
106
NO
RfV
r
11.7
t;
TEPK
ITERATIVE
CALCULATION
LOG
FOR
A BURIED
PIPELINE
AT.
I 1 SEGMENT
N’
l I I
I
I ELEVATION
LENGTH
I
I I
I
I
PI
I
I
m
I [
+m -
I I
I
1 Ta
I I
T2
l I
“C
I “C
I
‘C
l bar al
I
I
I
1 bar al
I
I Tl
I P2
I
I
L
4.
e I
I I
4
*. :
I I
4.
I
I
I
*’
I
4.
4.
.,
4
4
k
S U c c
I
S
E
I ( !
-
I
-
:’
I 1
I
PROCESS
BURIED
ETJ
PIPELINE
A,T
TEPtDOPmIPIEXPc5UR 9r
CHK
OATE
~08r;r~f.
LxnrWt
CALCULATlON
CALCULATION
SHEET
Sheet Z of 2
IrEM: NO.
:
JO1
No.
:
IREVI
J 1
C
lo
i : I B
[ Y,i,’ 4 -.f OTAL
PIPELINES Date : 2181
TEPlDPlEXPlSUR
.
4. LITERATURE
k
1
I
4.1.
LUDWIG
4.2.
CAMPBEL
4.3.
KATZ,
HANDBOOK
4.4.
CRANE
MANUAL
4.5.
“Equations
4.6.
“Two phase
kcal/h.m.
INFORMATIONS
VOL I chapter
2
VOL I ChaDter
predict
12
OF GAS ENGINEERING
buried
pipeline
A P computed”
“C
x o $j’l
R. Soliman
concrete
0.65
Wet soil
1.49
sand (dry)
0.30
2.98
sand (wet)
1.49 0.022
-> air
Ground
-> water
Epoxy coating Coal tar
29.8
Air
38:7 (2bd Water
7
G.King
Hydrocarbon
043 March ProcessinK
16, 1981 Aoril
1954
-3
1.19
Ground
chapter
temperatures”
Soil
’ Steel i ,
AND USEFUL
-
1.19
0.510
0.67 (0 .,,I? 0.22
t
6-s I
Joule-Thomson coefficient* -*w-m
h2
Specific >
1n
heats’ -1-m
-m--w 7
GLOBAL ENGINEERING
SHEO .
LIMITED iLlEN XJBJECT
PROJECT
JOB
No.Na..
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..._
___.___
- .
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.
----. . . . . -... - . .-.-
GLOBAL ENGINEERING LIMITED
._ .._
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SHEETNo.-
LIEN7
PROJECT
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CHK’D
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BY
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No.-
No..&
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‘!
i
-
TOTAL
PROCESS
ENGINEERING
DESlGN
MANUAL
TEP/DP/EXP/SUR
jr
.
-
ly-
12.
PACKAGE
UNITS
Revision
:
Date
:
Page No : 2/85
TOTAL
PROCESS
ENGINEERING
DESIGN
MANUAL
DEHYDRATION TEP
TEP/DP/EXP/SUR c
J
1. APPLICABILITY
For many in order
studies
undertaken
to reduce
there
the water
will
be a requiremenr
content
of the export
transportation.
Generally
this design
engineer
be aware
of some of the options
should
the dos and donts unit (TEG). glycol
The majority
contact,
2. GENERAL (English
of design
of this section
this being
phase to acceptable
be undertaken available
the most
widely
ur . n for pipelir1.
vendor.
for dehydration the basis sizing
is concerned
dehydration Limits
by a specialist
and also how to undertake
DEHYDRATION units
will
for a gas or liquid
However
schemes, of the most
with gas dehydration
some
tlof
. ,
commc
using tri-erhylen;
used.
NOTES
are used throughout
L
this section
for convenience) I
.
Gas is normally formation liquid
.
dehydrated
in gas transmission
water
iMethods
of dehydration
.
Absorption
(di- or tri-ethylene
3.
Direct
4.
Compression
5.
Chemical
hydrat
.
the gas is dehydrate of the line.
silica
gel, mole
sieve)
glycol)
cooling followed
3.
by cooling
reacrion
methods
(for method
have minor
of the advantages
injection
see 4.0)
usage and are discussed
and disadvantages
elsewhere
of various
absorption
in literature. liquids
is gib,n
iI
1.
Tri-ethylene
In order
glycol
is the
preferred
of di- and tri-ethylene to limit
glycol
viscosity.
Glycol
losses
run around
the overhead
glycol
used)
(0.0033
Total
to 0.012
operating to prevent
gal/M,MCF
(0.0016
losses due to leakage,
liquid.
ExampIt
temp
of 38 “C (10(
problems
.
m3/MMm3)
vapourisation,
*
due to the ’
,
due to solubilit)
m3/MMm3).
upto 99.1 % can be acheived
gas will be required.
absorption
are given in Fig. 1 & 2.
losses zi max practical
in the order
0.025 gal/lM,MCF
purities
widely
of 50 “C (50 ‘F) is recommended
are usually
of TEG
(most
glycol
2nd in the overheads.
Concentrations higher
Unless
to prevent
the flow capacity
2.
vapourisation
.
and reduce
in order
in usage are :
“F) is used. A maximum
.
at low points
corrosion.
(Alumina,
flowsheets .
and reduce
1. Adsorption
A ,ummary Table
lines,
may accumulate
The last three .
to 6 to 10 lb of HZ0 per MMSCF
, i
without
the use of stripping
gas. For I
TOTAL 1
eNo:
PROCESS
:-.
ENGlNEERING
DESIGN
Revision
MANUAL
:
0 f
DEHYDRATION Date
TEP/DP/EXP/SUR
Glycol
!
foams
prescrubbing
)n UT
* [
pelirer rt
.
meof
.
Actual
;
in the presence and addition
gas exit
equilibrum
dew point.
The number
iyleni
always
agents.
are usually
Take
of trays
prov:ded
12.2
by good feet
t
lo-15
this into account
Regenerator 4
in order
trays.
‘F
(5.5 - 3 “,C) above the theoretical
when setting
the specification.
to prevent
*
To prevent
rate
at lo-15
3.
,n ir
small
efficiencies
degredation.
Limit
condensation
heat
“Cl at atmospheric
pressure aim
pump capacity. in the glycol
feed maintain
still
column
the inlet
water
220 “F (104 ‘C) at top to prevent
should run at
temperature
rates should
SIZING
be between
2-4 gall/lb
HZ0 removed
on data
consumptions. hand method
1. Determine
water
lbs/MMSCF,
3 IS a good number.
CALCULATIONS
and
utility
loss of glycol
rejection.
be performed for estimating
2. Calculate
is
caps 33
flux to 5000 - 7000 BTU/hrftZ,
An exact sizing of a TEC unit will normally CFP inhouse program “GLYCOL” also exists
.
an excess of either
are 25 % for bubble
not be above 400 “F (204
at least 2000 BTU/gall
circulation
PRELIMINARY
following
(4 trays)
‘F (5.5 - 8 “Cl above the gas exit.
maximise
Clycol
is usually
Recommended
should
glycol
hydrocarbon
Regenerator but
height)
Use 24” tray spacing.
temperatures
for 6000. Provide
I
(or packing
in the design.
l/3 % for value
nplt
dew points
t his can be minimised
hydrocarbons,
of anti-foam
2185
;
mmc
drat
of light
Page No :
These
are based
can be used however content
of inlet
from
to estimate
gas to contactor
by the vendor on request. The vessel sizes, circulation rates the
BS+B
the required
design
guide.
The
size :
at required
temp
and pressure
Fig. 7
kgfiMMm3. total
water
maSs in feed gas to contactor
10( ’ 3.
‘he ’
O’ ) ’
4.
I
calculation
Calculate
dew point
Calculate
amount
5. Use 3 galls TEL/lb I
# I
Repeat
for exit
gas using required
depression of water
glycol
circulation
required
TEG concentration.
Use Fig. 4 to determine
required
stripping
Use 2000 BTU/gall
TEG circulated
(add 10 “F) contingency).
in contactor.
6. Use Fig. 3 to determine
7.
dew point
“F, “C.
to be removed
HZ0 evaluate
exit
rate. %
gas rate
to determine
reboiler
capacity.
PROCESS
TOTAL
ENGINEERING
DESIGN
MANUAL
Revision
:
0
i’
-Page No
c
T
8
DEHYDRATION TEP/DP/EXP/SUR
: 2185
Date
12.3
TEF 5.
3.
Use Fig. 6 to determine
number
and Fig. I to determine
contactor
9. Evaluate
contactor
tower.
Hence
estimate
A more detailed 4.
METHANOL
In order
height
sizing
dehydrated
method
can be found
in CAMPBELL
temperature
inhibitors
unit
is not
possible
is below
by injection
in previous
DEG,
the
point
TEG.
then recycled.
product
sections.
is normall\r
On some oc
of the
the inhibition
to depress the hydrate
are methanol, being
lines
due to the location
to hydrate
of inhibitors
the liquid
in base c
INHIBITIOl\i)
as defined
pipeline
KC pot
VOL II.
sieve this
integral
of contactor.
or mole
minimum
is normal,
include
,is gas transmission
to plant)
plant
2 vessels)
formation
(wellhead
Common
t
hydrate
however
.
in contactor
diameter.
(HYDRATE
in a TEG
This is acheived
required
(see section
weight
INJECTION
to prevent
of trays
source.
of water
and freezing
ior If th,.
is requires
points.
Recovery
of inhibitors.
at the
Economics
of methanol
recovery
receivin are no
favourable. .
.
i
Methanol
is adequate
limitations.
Above
Predict
injection
w=
for any temperature. - 10 “C better
rate
for hydrate
DEC not good below
as lower
vapourtsatlon
depression
ds follows
d:M 100 Ki + d M
- 10 “C due to viscositv
/
losses. :
I
w
=
weight
% inhibitor
d
=
‘C hydrate
M
=
Mel wt of inhibitor
Ki
=
1297 for Me OH
depression
1 I I.
2220 for DEG, TEG .
To use above equation
:
1. Predict
hydrate
2. Estimate 3. d .
The
amount
calculated + dissolving. Ib/MMSCF),
of inhibitor
injected
above and also provide Adjust
injection
vapourisation.
=
For
min flowing
temp
at max. press in line Tl
temperature
1
in line T2
6..
Tl-T2 must
be sufficient
for vapour
rate
formation
and liquid
accordingly.
methanol
For
use vapour
to depress
the hydrate
point
a
phase losses due to vapourisatioglycol
use 0.0035
pressure
charts
m3/Mm3 (CAMPBELL
I (O-Z- i pot’ 1
159).
,
I
L
,iOTAL 1
w NO
PROCESS ENGINEERING DESIGN MANUAL
Revision
:
0
I
Page No : I
DEHYDRATION
Date
: 2/85
12.4
-I i I i
.
5. SOLID Solid
. i i
3ase c
BED DEHYDRATION bed dehydration
can be acheived water.
j
Solid
is used when lower
by glycol
bed dehydration
the cost is competative INOTES
rmalJ\’
units.
residual
This is generally
around
facilities
.
LNG
.
Available
If th,:
quirec
always used molecular
dessicant
medium
icositb
Alumina
4-7
Gels
7-v
Beds
to acheive
1 ppm H20 or less.
Kg bed cheapest
9-12
Sieve
can be severely
the dessicant
: I
providing
: 4-6
salts and liquids. i
or 1 ppm resldua:
desifgn requirements
sieve dehydration
Bauxite
.Mole&ar .
rhar
to TEC.
KgH20/100
.re no
the - 40 “C mark
can be used for less srringenr
when compared
are required
:
ior
:eivin
conc$ntrations
water
degredated
It is essential
by heavy
most expensive oils,
amines,
to have a good feed filter
glycols
corrosion
or scrubber
prior
inhibitors to entering
bed.
.
Bed life is usually
2-4 years depending
on contamination.
.
Gas flow through
the bed is generally
downwards.
ensures the water
is stripped
from
the media
Regeneration
gas flows upwards.
having
to pass all the way through
without
Thir
the bed. Figures .
. - Tl
Regeneration
temperature
media,
too low results
Table
1 gives a summary
is usually
sieve arrangement. 175 “C
- 230 ‘C.
Too
high
temp
destroys
th<
in poor regeneration. of operating
USEFUL
REFERENCES
and regeneration
practices.
AND LITERATURE
6.1.
CAMPBELL
VOL II CHAPTERS
6.2.
HANDBOOK
OF NATURAL
’
6.3.
PERRY
(0.2, ‘i
6.4.
GAS DEHYDRATION
int
w
satio-
.6.5.
L 4
6.6.
18
tuning
existing
KATZ field
et al. Chapter
- World Oil - Jan 1981
C. SIMMONS
0 + CJ
“Cutting glycol costs II” “Correlation eases! absorber-equilibrum
line
“Cutting
glycol
Cost5
BEHR
I”
0 + VJNOV
7 1983
16
installations”
D. CRAMER
dehydration”W. I
17 AND
GAS ENGINEERING
“Fire
PDI’ I
-,
molecular
I 6.
-L
8 and 9 show a typical
Sept 21 1981 Sept 28 1981 tales TEG for
natural
ga!
L
TOTAL 1
PROCESS
DESIGN MANUAL
ENGINEERING
TEP/DP/EXP/SUR
Revision
:
*
Date
: z/es
Page NC
12.5 A
PER
CENY
UYCOL
ST WEIGuY
. w--e
----
Fig. (Cam&d/
Fig. (Campbd/
2
Aor and
*heat Laur.nc*.
for
nictttylm~
glycd
dehydrocior,
plod.
Flow
1 and
sheet
Iavrmce,
for
dicthylenc
glycol
dehydrotmn
plant.
IIINI?!'3 TEG CONCLVXATION
--
1.
Id u I.
rd.
._
..__ _-.--..~~~ F&l. 3 Id..4 .I
-L--L---W*, -
---------I-
co, -,
,, .e.....I -.A .,rrs,
, is
,
.
.-
I
I
Y
I I
I A
r
TOTAL
PROCESS
ENGINEERING
DESIGN
MANUAL
TEP/DP/EXP/SUR
---
..
“.--
_..._ :‘::--:.I-: --
.._ . .._
‘.-.::;.iI<; ‘;2i::;l:-7
..
i
FIG.
5
SIZING OF ABSORBERS
FLOWING
PRESibRi:-PSIG
_.
’ “I TOTAL 1
PROCESS
ENGINEERING
DESIGN
nevtslon
MANUAL
:
u
rdge
I
NO
I
DEhYDRATION
Date
TEP/DP/EXP/SUR
‘RAYS
OR PACKING
I
6 FOR
C’LYCOL
.
I 1
c
P / .-.. Y”--.-. C’.._-. -_‘. .y:.. . 3, -Sk f:!::. -7 -... -_. .-. 7..-
f ICUAE REOUIRED
: z/t35
I
: \ ’ (: ,
g:: ! !> , I
I
I
01 01234S678 CLYCOL
T O WATER
CIRCULATION
RATE
GALTEWLEHfo
! :--.. i . ..I.: v .: ........._ F..,.I ‘II x-!j
, , ,
w Lo lo A)
11J 40
-10
0
20
bo
40
loo
DEHV
1’ L.
ORATORS
E
:
-__
ToTAt
PROCESS
ENGINEERING
DESIGN
MANUAL
Revision
: O
Page No
Date
: 2/85
12.9
i I
T
DEHYDRATION
TEP/oP/EX~/SUR
I
I
7-E 1.
2.
3. F14JU
a
Basic
CharacccrLsclcs
Of ?iolccular
Sieves.
rI GAS TO et
OnlEo
OnTEn I" 1osOnCtlow
DRYGA1 I nECTCLIWC RECYCLED GAS CO~P~EssOw
.
No
PROCESS
ENGINEERING
DESIGN
MANUAL
Page No :
GASSWEETENINC 12.10
1. APPLICABILITY Generally
natural
(CO2) hydrogen To obtain eliminate
gas, or associated sulfide
(COS), carbon
a commercial these
sweetening
disulfide
product,
sour
components
gaseous
the development
this case CO2 is extracted
by a selective
for gas sweetening
on which system
given
A detailed
sizing
referenced
Ii terature
and lists
to select
method
is beyond
the
or liquefied, or process
mainly
carbon
dioxide
gas nfeeds to be created
reasons.
An other
of the CO2 injection
to improve
process.
details
their
specific
for
acid components,
(CS2) and mercapians.
for safety
with
available
is linked
gas contain
This
advantages
section
aspect
to
of gas
oil recovery.
different
and disadvantages.
In
methods
GuidelInes
are
services.
the scope
of this
section,
but can be found
in the
is required.
2. UNIT The specification
of treated
gas can be given in grains/100 1 grain/
3. GAS SWEETENING Various
chemical
-
physical
-
chemical
are available
: -
solld
absorption
-
conversion
CHEMICAL
process is the most
cryogenic
fractionation
utilised
ABSORPTION
the feed gas by chemical The main
bed adsorption
using catalyst
In this type of process,
-
100 SCF = 16 ppm volume
absorption
the absorption 3.1.
content
PROCESSES
processes
-
SCF for H2S or sulfur
chemical
the chemical reaction
solvents
solvent and releases
absorbe them
the acid components by heating
present
at low pressure.
are : Aqueous
The Alkanolamines
56 normally
used (wt)
-
.
MEA (Monoethanolam
.
DCA (RI (Diglycolamlne),
.
&IDEA
.
DIPA
or alkaline
Ine)
15-20 (FLUOR
ECONAMINE)
up to 65
(Methyldiethanolamlne) (Diisopropanolamine), salt solutions
1x30 (ADIP)
as potassium
30-40
carbonare
K2CO3
25-40
in
-
Alkanolamines . close
cannot
be used undiluted
to solid state
at ambient
. low stability
at high
gases) with
generation
Table 3.1.1.
MEA
(heating
of highly
MEA PROCESS
products
and a&advantages
solution
the absorbed
ac
:
by decomposition.
of these
processes.
1)
wds the first
15 56 weight
It‘ to extract
is needed
corrosive
(see figure
solution
:
conditions
temperature
1 shows the advantages
because
solvent
used and is still
widely
used. Generally
a
is utilized.
a) Advantages - high reactivity - good chemical
stability
-
low solvent
-
pubicly
cost
available
licensing
(no
fees)
b) Disadvantages - irreversible
degradation
into
corrosion
products
by sulfur
components
such as COS, CS2 - irreversible
degradation
for the solvent
by oxygen
(Direct
contact
witl.
air must be avoided) - ineffectiveness - high utility - no selectivity Fields
mercaptans
requirements
- need of reclaimer
c)
I
for removing to purify
-
high vaporisation
the circulating
for absorption
between
losses
solution
H2S and CO2
of utilization
- general
use : MEA
15 % volume gas partial
acid pressure
MEA unit is around
can be utilized gases without
for gases containing COS,
up to 100 PSIA
CS2,
mercaptans
currently
maximum
from
60 ppm to 1
and with capacity
acid .. for
the MEA
I
most
widely
used gas treating
process and some improved
Flow diagram
1
250 X106 SCFD.
3.1.2. DEA PROCESS The second
a
very similar
process
processes
with
a tendancy
I
exist,
to MEA process without
to replace
reclaimer.
SwEETEN1 zPFPTf!k 1 cAs Date :2,~; pag PROCESS
le NO 12.11
‘I t 1 i 3 ac
DESIGN
-
no degradation
-
a significant
by COS and CS2 (hydrolysed amount
-
a good chemical
of the light
-
a very low absorption
-
publicly
lower
of hydrocarbons
compared
an irreversible
degradation
-
higher
requirements
-
no selectivity
utilities
to MEA
system
-
H2S
and thus higher
(Not applicable
between
circulation
to SNEA-DEA
of the solvent
for absorption
process
content
treated
is used to treat
of the
rater
process)
by oxygen
H2S and CO2
1. Split
treated
gas can be as low
gases containing
acid gas confent gas lower
(4 ppm volume)
process depends d) Imoroved
acid ..
vaporisation
of utilization
requirements
n to I
- reduced losses
COS, CS2, RSH (up to a total
I
on the feed gar
- no need for a reclaimer
available
reactivity
The DEA
I
present
b) Disadvantages
c) Fields
I
into CO2/H2S)
mercaptanr
stability
for the conventional
witl.
0
is absorbed
-
7ents
Hevtston :
MANUAL
a) Advantages
1 j
ally a
ENGINEERING
of 20 % volume)
than
can be acheived. as to 100 ppm
on the CO2/H2S
ratio
H2S, CO2 and alsc
the
normal
The CO2
volume.
specificatior content
Performance
of the of the
in the feed gas.
processes flow (see figure
For sour gases with
2) high
acid
gas conrent
(above
25 % mole),
flow rate can be reduced. Investment cost increases (more equipment, conlplex columns, increased regenerator
DEA
significantly height).
0-l 2. SNEA - DE.4 orocess I
SNEA
company
has developed
a process
using
a higher
concentratior
of DEA (above 30 % weight).
lace I
The process
licenser
claim
to give
in one step,
0 to 35 % of H2S and 0 to 35 % of CO2, most stringent
H2S specification
for gases containing
a treated
(4 ppm by volume).
gas matching
the
TOTAL TEPIDPiEXPISJ
PROCESS
ENGINEERING
DESIGN
MANUAL
GASSWCETENINC
R
3.1.3.DICLYCOLA~IINE
(DGA)
PRXESS
(FLUOR
Revision
:
Date
: Z/81
1
0
I 12.13
‘;
ECOSri.ilISE) I
The
DGX
process
has
a limited
number
of
units
comepared
LIE?,
wlfh
an I
DEA. Although
in rhe
refered
KO as the
to compare a)
low
-
.11E.\
solution
low
process
are
was
process
developed
by FLUOR
advantages
and
and
i
disadvantage:
:
rate
due
to the
during
the
concentration
(same
abs
tio
as MEA) consumption
Disadvantages -
needs
cooling
-
high
solubility
-
high
solvent
Criteria
hydrocarbons
and
absorption
aromatics
pnase
are
dissolved
cost.
&MEA,
DCA
The
1.5 to
30
operating 3.1.4.DlPA
of rhe solutron
of selectron
required.
reacts
process
both
with
is applicable
5% volume
and
pressures
above
has
developed
CO2
and
to gases
C02/H2S
ratios
CS2
with
and
acid
a
gas
between
300/l
reclaimer
is
content and
from 0.1/l
I
at
15 PSIC.
I
PROCESS process
been
It is characterized 3.1.5.MDEA As
the
EC\3NA&IINE
circulation
utilities
Like
This
FLUOR
with
capacity
cl
domaine,
Advantages -
b)
public
by the
by SHELL
selective
under
absorption
the
ADIP
trademark
of H2 in presence
name.
of Co2. I ,.
PROCESS with
DIPA,
of co2. 6 !VDEA processes -
SNEA
-
UNION
I
‘IDEA
are
is characterized
proposed
(D) CARBIDE’:
UCARSOL
by process
by its
selectivity
licensers
:
for
Hz5
in presence
i I
TE
I) TOTAL 1
e No
PROCESS
ENGINEERING
DESIGN
Revision
MANUAL
:
I
PageNo: Date
: 2185
T
12.13
3.1.6.HOT
POTASSIUM
CARBONATE
PROCESS
(see figure
I
12.14
3)
.
An activator 4 an
reactivity
specific
i
(amine
- CATACARB
Irage!
’ I
and other
licenser
is added t
(amine
main
and other
I’ t.
regenerator
operate
‘! I ‘I
a) Advantages
increase
the
activators) (arsenic
characteristic
to
activators)
- CIAMMARCO-VETROCOKE The
tio
process
of the solution
L BENFIELD and
to each
of
the
and others
process
activators)
is that
at the same temperature
the
absorber
and
the
(1 IO/l lS°C)
-
no degradation
by COS and CS2 which are hydrolysed
-
good-chemical
stability
-
no reaction
-
low hydrocarbon
- no need for a reclaimer
with air
- low heat requirements
absorption
- selective
(isothermal)
CO2 absorption
(ClAMMARCO) b) Disadvantages
er is
-
licensing
fron
-
low reactivity
- high water
fees required with H2S
content
- no mercaptan
of treated
gas
absorption
‘1 at c) Fields
of utilization
1: Applicable ame.
makes
I
it difficult
Generally ..I encc
(
This
mainly
to achieve
dual
attractive
high
(amine
-
generally
be in
some
instances
more
process.
utilized
can have a strainless
can be stainless, cost1 1, copper
can
for H2S removal
MATERIALS
steel
Regenerator
Low H2S absorptior
of 4 ppm volume.
amine
/ K2CO3)
cost wise than an amine
3.1.7.CONSTRUCTION
content.
will be used
for CO2 removal system
CO2
specification
a two stage process
K2CO3
Carbon
on gas with
but still
alloys
subject
in steel
the cladding
to corrosion.
shall be avoided.
chemical
absorption
and trays. Monel
Reboiler
is an alternative
units tube: b;
TOTAL
PROCESS
ENGINEERING
DESIGN
MANUAL
Revision
:
Dare
: 2/85
Generally
solutions
treating
gas with
high
CO2/H2S
When
~111 be more I,I
t
the
following intern&, PHYSICAL
12.15
ratlo
corrosive. CO2IH2.S
ratio
equipment
:
regenerator
is high,
stainless
steel
will
exchanger
amine/amine
trays and reboiler
be preferred
tubes,
for
expansion
the ,: value im
tubes. I
ABSORPTION
In this type contact High
page NO :
CASSWEETENINC;
TEP/DP/EXP/SUR
3.2.
O
of process,
and releases pressure
advantages
the solvent
them
by simple
the acid components
expansion
and low temperature
and disadvantages
especially
extracts
favour
solvents.
in the case of high acid gas partial
Nor suitable
for sweetening
large
of heavy hydrocarbons.
amount
The main
processes
physical
; I.
at low pressure. the physical
of physical
by simple
absorption.
These
processes
pressure: (above
at low or medium
pressure
Can be considered
Table
2 lists
the ,
are applicable
5 bars also).
I
(10 bars abs) gases containing for a selective
,
absorption.
are : I
3.2.1.
WATER
WASH
Can be used as prrmary by addition
3.2.2.
of trays
treatment.
of its low efficiency,
a large
amount
considered
carefully.
SELEXOL
PROCESS
-
developed
water
wash can be realized
H2S.
water Corrosion
wash should prcblems
be used mainly for
this
on gases
process
should
a’ IAitc,
be I I
(see figure
by NORTON
I’ I
4)
CHEMICAL
PROCESS
can be applied
to gase:
with large acid gas content. -
-
has been applied
for sweetemng
of gases conraining
and 9 % of H2S at pressure
ranging
treated
can reach
gas specification
used to absorb selectively -
other
1
in the top section.
Because
of
For absorbers
sulfur compounds
from
up to 65 % of CO;
25 to 100 bars abs.
0,02 % CO2
and
1 ppm H2S.
H2S or CO2 it can also dehydrate. (COS, mercaptans)
are also eliminated.
Wher
rTOTAL 1
PROCESS
ENGlNEERlNG
DESlGN
3.2.3.
FLUOR
Date
:2/M
SOLVENT
- developed
intended
volume
residual
- CO2
12-16
.
by FLUOR,
- primarly
I
:
LASSWEETENING
TEP/DP/EXP/SUR
norf
Revision
MANUAL
propylene
carbonate
for the removal CO2 content
solubility
is higher
is used as the solvenr
of CO2 from
around than
1 % volume
that
gas containing in treated
obtained
up to 50 %
gas.
with
MEA
and CO2.
H2S
or
potassium
carbonate. ical
- can
I
be used to treat
require
mercaptans
the , :ble
a finishing
;
- requires
I
3.2.4.
treatment
H2S
douwstream
to obtain
content
would
6 ppm of H2S. COS and
also absorbed. an extensive
PURISOL
gas containing
use frotating
equipment.
PROCESS
.ing - proposed
I
by LURCI
- as the solubility
of H2S is higher
process to remove
I 3.2.5.
RECTISOL
uses n-methyl-2-pyr-rolidone
as solvent
than CO2 can be considered
H2S even in case of low H2S/C02
as a selective
ratio.
PROCESS
:ed i - developed High
by LURGI,
selectivity
gas (cooling be
i I
- major
for C02,
by an external
disadvantage
equipped
uses a refrigerated
with
primarly
of methanol
used on synthesis
refrigerant
cycle
of the process, refrigeration
solution
gas or on precooled
for example).
when not integrated
cycles,
as solvent.
needs
in a plant
refrigeration
already
and
methanol
as solvent.
Selective
injection.
I’ I 3.2.6.
ESTASOLVAN Developed process stringent,
3.3.
PHYSIC0 3.3.1.
by F. UHDE for
CMBH
H2S extraction.
additional
- CHE.MICAL
uses tri-n-butylphosphate If CO2
unit downstream
specifications
on the
treated
gas are
will be required.
PROCESSES
SULFINOL - this process has been developed - ir. loIves a physical (DIPA alkanolaminel
by SHELL
solvent (sulfolane) in aqueous solution.
and a chemically
reactive
agent
TOTAL
’
PROCESS
ENGINEERING
DESIGN
MANUAL
Revision
:
0
Date
:2/85
Page No .
GAS SWEETENINC TEP/DP/EXP/SUR
Suifolane
permits
extractron -
3.4.
for
selective
operating
conditions
process
also permits
(COSL
As for
occurs
of CO2 and H2.S. Amine
of the acid gases from
performances
-
deep absorption
(mainly
processes,
SULFINOL
solution
of mercaprans
absorption,
aromatics).
to amine
during
and non selective
extraction
physical
solvent
Does not dehydrate
SULFINOL freezes
SOLID
BED PROCESS
3.4.1.
MOLECULAR
SIEVES
-
not widely
used for gas sweerening
-
can be used as a finishing
-
absorption
and other
compound:
of
sulfur
heavy
rhe treated
1i 1 /
or
‘;
gas. Comparea
*
tendency i
-2°C.
treatment
to remove
mercaptanf
sieves is parricularly well adapted to obtan the sulfur content specifications
treatment
I
hydrocarbon:
in molecular
finishing
rht
depencs
shows a low foaming at about
facillrares
regenerarion t H2S absorption
absdrption
TEPf
12.17
for
LPC
as
4
of propane
and butane
-
good
absorption
capacity
for
H2S
low
for
C02.
They
remove
water
preferentially 3.4.2.
sieve life
IRON -
is reduced
SPONGE
could
PROCESS
be also classified
(H2S is converted
4. CRITERIA -
there studied
-
final
applied
mainly
-
discontinuous
process,
Spontaneous
combustion
is no multipurpose
I as absorption
process
or as a conversion
process
to sulfur)
-
FOR SELECTION
I
for gases with high CO2 and H2S content
I
to gas with low H2S content iron
oxide
has to
of the fouled
be regenerated
product
or replaced.
I
occurs with air.
I
OF ABSORPTION PROCESSES process
for gas sweetening,
each case is specific
and shall
be I
accordir3gly selection
is done
which seem appropriate
on the basis of economical to satisfy
the treated
criterial
gas specifications
from
short
list
of processes I
5. R
“TOTAL
re No -
1
0 I GAS SWEETENING
Date
lEP/DP/EXP/SUR
h2.17
chemical
processes
influence
of the gas pressure.
physical
processes
performances
pressure
with
acid
ound:
chemical
processes
.rbon:
selection
criteria
processes
but shall not be considered
ias or
parea -
are characterized
high
4.1.
CO2 ABSORPTION
4.2.
SIMULTANEOUS
4.3.
H2S ABSORPTION
listed
4.4.
They require
gas partial herebelow
ABSORPTION
H2S SELECTIVE
are
ability
a large heat quantity
more
dependant
pressure,
the
can
be used
absorpyion for
is berter
preselection
At than
high for
of sweetening
as definitive.
(NO CO2 IN THE GAS) (see figure with natural
ABSORPTION
for regeneration
on gas pressure.
5)
OF CO2 AND H2S (see figure
situation
12.18
to absorb acid gases with a low
(NO H2S IN THE GAS) (see figure
This is not a frequent G as
by their
: 218s
(H2S AND
6)
7)
gases. CO2 IN THE GAS) (see figure
8)
Ipane Physical
soivents
ark particularly
well adapted
in this case.
dater Among
xess
/
5. REFERENCES
(1) I
Iced.
I
Natural
II be I fsses I
I
I
only
AND USEFUL
LITERATURE
gas production
transmission
F.W. COLE, (2)
Gas
D.L. KATZ,
conditioning
ROBERT I
processes,
MDEA
and DIPA
seem
to be adapted
and
liquid
for this
service.
I
I
the chemical
N. MADDOX
and
L.S. REID,
and processing C.H.
processing edited
by JOHN
HINTON
(volume
4)
gas
M. CAMPBELL.
sweetening
by
TOTAL ( TEP/DP/EXP/SUR
PROCESS
I
ENGlNEEd;NG
DESIGN
MANUAL
Revision
: 0
Date
: 2/9sJ
Ca.s SWEETENING
UEA
PROCESS
FLOW
OIAGRAU
SWEETGAS A
51 r--
=I. r-’ 0
STILL.
L..P. _ 00.I
= 20
/
= 20 ‘-7
..-
El
I FLASH
i
TAN*
r
05( STEAM El
h
)
L
RICH
MEA/ LEAN EXCMAnGEA
YEA
STILL PEBOILER
REFLux
PUMP
? No Datk
TEP/DP/EXP/SUR
SOlJR cG--
SPLIT
STREAM
.~MINE
PROCESS
I,
: 2/85
12.2c-l
PROCESS ENGINEERING
DESIGN MANUAL
? t
TEP/DP/EXP/SUR
13,
UTILITIES
) r;“rnz. .
:
a8j
beNo:
iJ
T
‘TOTBb:
i PR’OCESS ENGINEERING
MANUAL
DESIGN
Revision
:
0
Date
: 2/85
page No :
UTILITIES TEP/DP/EXP/SUR
13.1
1. APPLICABILITY For both feasibility estimate
and pre-project
of utility
requirements
studies
the engineer
both in consumptions
This section details a few guidelines
will
be required
and equipment
and notes on the following
to make ar
rgquired.
utilities
:
WATER TREAT,‘vlENT UTILITY
liND INSTRUbIENT
t\lR
INERT GAS GENERATORS WATER SYSTE.LlS FUELS 2. WATER TREATMENT The
following
details
of effluent
quality
API gravity
settler
.
Usually
water treatment
equipment
given in order
:
the first
any floating
the common used effluent
line of clean up. Simply
oil or debris and a bottom
quality
a settling
tank with a top skimmer
to remove
skimmer to remove sludge.
.
Effluent
around 150 microns globules and 150 ppm oil.
.
Large bulky items, cannot be used offshore.
.
Simple, cheap very common in onshore use.
Tilted Plate Separator
(TPS), Corrugated
Either
circular
or rectangular
in design. ,
Plate Interceptor
(CPI) ,
.
Widely used both offshore and onshore.
.
Uses plate packs, usually at 4s” mounted oil + water within Effluent
.
Can have problems with hrgh solids content
.
TPS units are u;ually
.
settling
between,
the spaces between the plates.
.
Flotation
quality
in a tank and relies on gravity
I
down to 60 micron oil globules and 50-200 ppm.
used as the first
if upstream
treatment
settling
tank is not installed.
! 8
stage offshore.
units -
Uses induced or dissolved
air flotation
Works in reverse to a gravity ank).
settler
to remove any residual solids/oil
in the effluent.
(small air bubbles trap debris and float
to top of 1
PROCESS ENGlNEERlNG
Revision
DESIGN MANUAL
:
0
I
Page No : I
UTILITIES
. .
Effluent
quality
better than 40 ppm. Vendors usually guarantee
Can be used both offshore
and onshore. Usually
installed
.
units
either
achieve water quality .
.
Usually
not
content
enforced
systems only)
uses media or filters
required
IMore commonly required.
for
beds (sand, anthracite,
garnet,
effluent
water
by local effluent
standards.
used for water
re-injection
Can achieve l-2 ppm in certain
treatment
shells) to
unless very low residual
where high quality,
solids
low solids level
is
beds, IO-15 ppm is more common.
Units are generally
compact but heavy due to media bed weight.
.
Good pre-filtration
is required
to prevent fouling
up of main bed units.
standards
Listed below are maximum
residual oil content
NORTH SEA INDONESIA
in effluent
LOCAL
water for dumping to sea :
40 iv-n + MIDDLE EAST
30 wm
CHINA
20 wm
5 ppm (European standard)
ESTUARY (river)
Process drains, produced water, deck (site) drains (see figure .
walnut
(fibre socks, mesh, stainless steel cage).
.
Effluent
of a TPS unit or
f
(Use for Water injection
Filtration
13.2
< 30 ppm.
downstream
API separator. Filtration
?/85
Date
TEP/DP/EXP/SUR
Produced water may need degassing before treatment.
1) If the amount of dissolved gas is
small it may be possible to handle it in the TPS unit. .
Deck or site drains normally
flow to a separate sump tank before de-oiling.
If the deck
dralnage is small or produced water flow is small can combine both streams through one TPS unit. .
Process drains are normally
manually
tank. These drains are generally .
Always oil-water
try to use gravity separation
arrangements.
c
initiated
to the return
oil stop
water free.
feed between units.
harder.
and pass directly
Similarly
avoid
Pumping can cause emulsions and make fast
flowing
lines
and turbulent
pipe
TOTAL
&ES
(
ENGINEERING
Revision :
DESIGN MANUAL
Date
AND INSTRUMENT
Compressed utility
services eg : pneumatic
For turbine/engine
.
For general instrument
.
Consumption generally
air)
for instrumenr
tools, cleaning,
start-up
control,
turbine
and engine start-up t
etc. :
air, compressor
an
discharge around 9 bar is adequate.
for each air pilot (= valve)
0.8 scfm (0.022 m3/min)
for valve positioner
1 m3/h per valve unit will do as first estimate. capacity
air : consumption
for design.
is intermittent
and difficult
Add 75-100 scfm (130-170 m3/h) to compressor .
All plants should have 100% instrument
.
Utility
and instrument
depending on capacity .
13.3
17-25 bar supply will be required.
and utility
Add 25% to compressor Utility
: 2185
2)
: use 0.6 scfm (0.017 m3/min)
(instrument
.
AIR (see-figure
air is used on plants
.
Page NO
UTILITIES
TEP/DP/EXP/SUR
3. UTILITY
0
Instrument
to estimate
capacity
for initial
at early project stageestimate.
air standby capacity.
air can be supplied
from
same compressor
or separate
requirement.
air must be dried before use. Dew point of air is dependant on minimum
temperature
one!
in location
of unit. Generally
air
dessicant bed driers are used giving dew point
as low as -60°C. .
Size air receivers
to give lo- 15 minutes
down. Pressure in the instrument
of instrument
air receiver
air assuming the compressor
gee
should not fall below 80 psig (5.5 bar g)
during this period. .
For long air transmission
.
An estimate
of compressor
4. INERT GAS GENERATdRS Inert
gas is required
requirements
headers in cold climates
intermediate
KO puts may be required.
and dryer weights and power are given in figure 3.
(N2, CO21
in all
plants
for
purging
and inerting
of equipment.
For small*
N2 bottles can be used in racks, this however is not feasible for large units ant
so gas generators
must be supplied. The main types of generator . - cryogenic
distillation
- oxygen absorbtion
in use are :
-
of air on sieve
’
- gas combustion .
For purging purposes estimate 11 be purged in one hour.
capacity
based on 3 times the volume of the largest vesse’ i I
UTILITIES
TEp/DP/EXP/SUR
.
Cryogenic
distillation
is used only
Date
for large
volume
requirements, .
plants. Not used offshore. .
Gas combustion
produces a N2, CO2 mixture
for inerting
Pressure swing absorbtion mounted
units
are sometimes
supplied
existing
plant
air
for
production .
is the must common
compressor
with
LNC
for N2 generation.
used method
dedicated Air
supply.
specifically
and purging purposes. Not used c
much these days except for onshore large volumes. .
13.4
: 2/85
air
consumption
compressor,
Skid
or can use
‘is 4-5 times
inert
gas
rate, residual 02 in gas is l-2%-3%.
Details and weights of common units are given in figures 4 and 5.
5. WATER SYSTEMS Seawater Used for cooling
purposes both onshore and offshore.
sanitation
water and feed to potable water units.
Seawater
is also used for fire
seawater
cooling
circuit
water
is normally
Can also be used as wash water,
systems but is usually ‘a separate connected
to the fire
water
system.
The
ring for emergency
supply only. Always
coarse filter
the seawater
before
circulating
to the plant.
This removes any
debris or marine life. Treat
with
chlorine
at l-2 ppm concentration
- maintain
a residual
Cl’
level
in the
water exit at 0.3-0.5 ppm. Seawater
exit temperatures
to outfall
canals or drain caissons should not be above 4O’C
to prevent corrosion. Once through
systems
are preferred
for
small
cooling
duties
with only
exchangers.
For large duties and number of units where the cost of corrosion
prohibitive
consider
25%
using a closed
loop cooling
medium
system.
using
titanium
3-4
proofing
Common
is
used is
TEG in water.
For cooling
medium/seawater
exchangers.
These are especially
requirements.
I
water
exchangers
consider
ideal- offshore
due to reduced
or similar weight
plate
and space
TOTAL
PROCESS ENGINEERING
DESIGN
MANUAL
Revision :
0
UTILITIES
TEP/DP/EXP/SUR
Date
Potable water Depending
on location
for srorage, or taken direct For onshore Problem
plants
with
water can be made in sit% or supplied by tanker
of plant potable
from a mains supply.
most common
method
these units is size and weight
Solids) is 5-10 ppm. This results is a bland Increasingly
of water
maintenance
than
Organization
TDS for
evaporative
Power consumptions
units.
drinking
are high and residual
distilled
Water
water
Distillation
unit offshore
unit
quality
(EO)
unit
and need
is 400-500 TDS (World operating
costs
less
Health
of RO un’
is
RO units are relatively
3.5 kw
NO) . 5
kw
(VC) 15
kw
I
at present is the VC unit which is very reliable
Unit operates at IOO’C and is more
parts for servicing. .
Dissolved
distillation.
Vapor Compression
.
TDS (Total
water which is not pleasant to drink.
is 500-1000)
Reverse Osmosis
Most common
distillation.
: for a 100 gph (0.38 m3/h) unit.
Evaporative
operate.
is evaporative
popular now are Reverse Osmosis units (RO) which are lighter
1.5 times that of evaporative
.
supply
new, operate
susceptible
at ambient
and easy
to
I
to corrosion.
temperature
and has few mechanical
.l
Average membrane life is 3 years.
Consumption
: estimate
on 50-60 gallons per day per man (0.2 rn3).
Storage
: allow IO- I5 days for offshore
units
10 days for onshore remote areas .
Potable water can be dosed with hypochlorite
at 0.4-0.5 ppm to inhibit
bacterial
growth.
Waste water and sewage I’
.
.
Before discharging
to river,
sea, or underground
to meet local health regulations
prevalant
Limits
(Biological
are
imposed
Demand), coliform Example limits
on BOD
bacteria
are :
sewage + waste water
must
be treated
to the area of siting. Oxygen
Demand),
COD (Chemical
Oxygen
I
count and TDS.
bacteria
< 200 per 100 ml
TDS
< 150 ppm
BOD
< 100 mg/l > 0.5 mg/l < 1.0 mg/l
CI- residual
I ! I I
I
TOTAL
PROCESS ENGINEERING DESIGN MANUAL
Revision
:
Date
Z/85
’ Page No :
0
UTILITIES TEP/DP/EXP/SUR
-5 --
.
Sewage
is treated
by physical
artrition,
airation
and
chlorine
dosing
13.6
to 30-40
ppm
rav,
sewage.
tker
.
Provide
-
AUOW
15-29
hr retention
time
for
enzymic
action
to reduce
BOD.
’ 30-50
wastes.
gall/day
Use upper
per
limit
person
for
(0.15
m3)
hot unsociable
for
sewage,
show%r,
laundry
ano
kitchen
climates.
Ion. ved
6. FUELS
<. Diesel ess .
Jth
Used
for
emergency
alternative
is I
.
For
fuel
generators,
for
emergency
Pumps
motors
individual
day
and
air
compressors,
sized
on providing
cranes,
and
turbines.
equipment
provide
tanks
fuel
for
24 hr
operation. I’
.
[Main
diesel
tank
on location
(for
of plant
feed
to day tanks)
and normal
supply
should
hold
IO-12
days
supply.
This
is dependant
periods.
I .
Diesel and
to I
should smaller
I
.
For
This
boat
debris,
5 ‘&iicrons.
Can
is especially seawater
be centrifuged
recommended contact
to remove
offshore
and
poor
where
supply
residual longer
quality
can
water storage lead
to
problems.
storage
pedestrals,
I/
to -
particles.
supply
times, operation
xl
be filtered
use
atmospheric
platform
legs
venting
or inter-deck
tanks space
with
for
vacuum-PSV
offshore
storage.
turbines
and any
vent.
Use
crane
Gas
1
7.
.
Fuel
.
Always
1,
gas is supplied pass
10 microns his own
ed I’
.
FG
through
(generally
filters)
it\aintain
as normal
to generators,
a scrubber
turbine
- do not
FG
fuel
rely
temperature
before
manufacturer on this
at least
Filter
use.
will
state
quality
and provide
separate
15°C
dew
above
gas
supply
required
treatment
point.
gas driven to
motors. turbines
and may
include ’
anyway.
Minimum
to
temperature
of gas
IO be 5°C. en I .
Common
.
Size
supply
fuel
gas
pressures supply
are
on
15-20
maximum
bar (some design
jet duty
engines of
all
need users
35 bar). operating.
Allow
+ 10%
margin. .
FG used gas straight
for
flare off
purge
and pilots,
scrubber
overheads.
etc.,
does
not
need
to be filtered
to 10 microns
- use
TOTAL
I
PROCESS ENGINEERING
DESIGN MANUAL
UTILITIES
TEP/DP/EXP/SUR
I F‘recess
water
1 Compressed r
and deck
Air System
diain
water
treatment
lge NC
TOTAL
PROCESS ENGINEERING DESIGN MANUAL.
EST,MATE
1600
Page No :
0
UTILITIES I
TEP/DP/EXP/SUR
3
Revision :
.:.-.
:-
..:-.._- ., .:l
::.
OF WEIGHT
-.
; y.;
Date ’
J:.-.:;
r
f ICURE POWER
AND
3 FOR
INSTRUMENT
A4R
: 2/85
L
13.8
UNITS
_:..
‘: 1 ..z
2:.r /:.
*
.. : “-. ~~~~~~~~~~~~~~-;;~~~
_ ,2;--::, II.-...= yzI-=:.=
:-..---;.” -5
.=;;.ry:T.=.-
,
-. ,.
-
..
z;zi:---‘; ;=;-:.:..E:. z-.‘-‘::-+yr:.-:...-
- ‘-
;
._‘.Y=
:.-
:
;
-‘&
,.
~.
I
i
“-i
:
;:..
:
.-:
.:..
.: . ..;.;&zzc=tr::...;:
:ci;ci.:‘;i<jf: I
-
.~:::;:::L::~-.~:.:~
..
.,:
.!
,
:
.i 1..
i I.-..
-r’-
-‘i_---
1
.ij.l:.
~~--~,
. . ..m------.---. ..-....-.-..---.. .-.--::: -_.. ..__...-.
::,
: :..
..---.-..:.-
-. .---
..
-.
::‘
:y&
- -_.-. _.. .. ...-... ~-::,-::r:--:li’.-;i:.~::.
:
.
-0 200
300
do0 CAPACITY
so0 Nm3/h
600 (0’C
Layout plan
+ 1 bwrl
700
600,
900
1000
0, lcsidurl in ptodoct
wnltnl
Technical data Small
plank
Type dtsiwlioo
Rudy.fotoptnlion plant8 in one unil Fully fwdoo. md pctformmu.lcslrd. No ituullttioo vott No wditq watt tcquitrd. Mu 0,Y mnmnl
~yu~uc’
ill produL-4
pnyy
DwNl@
i’ 1
DWN SO DH’N c
Ptocz,s
ptcctutr
I IS 9
I: 10
OS : 0 ~---‘--G
SO-.
:
E
DH’N
Laqc
110
plants:
la ptodltd
K
2
3
II0
w
UO
Rudyktaprntion ,.tinlmd ilUU”JllOO
plmu WOtt
Mu 0,Y
;,,;uo$td qurnlity
fuoclion.tzsttd
ptrrw~;S
I I
:z NO
111
05 :
410
III
700
1600
0% :
70 71 lb
. -. _ . _. -
. ..__.
--
.-.._
. . ..-.._____.
_-
_.-
---.---
quanut, Y.!z!
Caol~ VIICI “l’h N, ptodua ptc,tutx 4 S bat b bar
ptcs;u&,brt
--
wntump~wn ql,W”h IW ---..-.. I70 IW
loo
.-
..---
-. - _-.
I: IS . . . ---------A-
ii II
11
190 410
450
t;;u$c~
ii II0 -- ----.... IKKJ 1440
E
.
41 4k
.--_..
unik
Ct Sal ---
I:!
$10 610 910 Ill0 Ill0
bat
consumption rppro.. LW
~A!!2 05
DH’N 400
from
---.-
--..
---
.-_- ---.--_--
:: __ .- _-I9 .. IfI
:; . __ ho
05 I
CO”lC”l, in ptoducl
DHH
I
6 bar ptcstutr PtJvct WtUUlllpllO” ,pptol. LW ---. . . . ..- -II.5 II
----_-._ 14 .-.
8% II) ____.__ II0 WI
drriyvtiun
DWN
1: . lo II :i -_______
TYQc ---
qqfh_---.
ii _._-__ II
W
bat
0, residual wolcol
.pptorLW
--
-
_-_-----~J;$o$FI ” qunur)
j;S bu * catuumplion
,
----
ptyc
---
lwl
_.._-._.
:I ;: ml II -. ..-._ - .--.-.-.510 510 :: 610 (I 41
.-.-..
_
_ __.__
ii
-.
:: 11 I
.-_
TOTAL
PROCESS kNWNkkHlNG
DESIGN
MANUAL
Hcvtsron :
*-- .r
TEP/DP/EXP/SUR
Date
I
. P
i.
..
15,
DATA
: 2185
Page No :
TO?‘AL
PROCESS ENGINEERING DESIGN MANUAL -: ..DATA
TEP/DP/EXP/SUR
General data Conversion tables
10
PSEUDO
17 18 19 20 21 22 23 24 25
Figs.
1-3 4 5 .6 7 8 10 II 12 13
30 31 32 33 34 35
36 37 38 39
42 43 44 45 46 47
48
t
AND OIL PROPERTIES
Physical properties of hydrocarbons Compressibility factors of natural gas Pseudo critical pressure VS. MW Critical constants for gases and fluids Critical temperature VS. normal boiling point Characterised boiling points of petroleum Fractions Molecular mass, BP, and densities of fractions DENSITY Relative Relative
density density
of petroleum of petroleum
VISCOSITY Viscosities of hydrocarbon Viscosities of hydrocarbon ‘ASTM viscosity chart
fractions fractions
VS T
VS MABP
gases liquids .;
VAPOUR PRESSURES Low temperature vapour pressures ,High temperature vapour pressures True vapour pressures of petroleum Hydrate formation pressures
18 19 20 21
SPECIFIC HEATS Specific heats of hydrocarbon vapours at 1 ATM . Heat capacity correction factorsSpecific heat capacity ratios at I ATlM Specific heat capacity of hydrocarbon liquids
22 23 24
THERMAL CONDUCTIVITY Thermal conductivity of natural gases Thermal conductivity ratio for gases Thermal conductivity of hydrocarbon liquids
25 26 27
LATENT HEATS OF VAPOURISATlON Latent heats of various liquids Latent heats of hydrocarbons Heat of combusion of liquid petroleum
40 41
CRITICALS
14 15 16 17
26 27 2s 29
Date
I
2 3-9
II-14 15 16
SECTION
28 29 30 31 32 33 34 35 36
: products
and oil
,
fractions
SURFACE TENSIONS - MISCELLANEOUS Surface tensions of hydrocarbons Dew points of natural gases Solubility of natural gas in water and brine Solubility of methane in water Solubility of natural gas in water i Solubility of water in hydrocarbons Temperature drops for expanding gas Temperature drops for expanding gas Physical properties of gas trearing chemicals Physical properties of water Physical properties of air
L .
0
-iUIAL
:
~‘HuL;~S~ tNUlNttHlNG
DESiGN
MANUAL
TEP/DP/EXP/SUR
Revision
:
Page No :
Date
:
15- lo
-I
,
.
,
:i P
TEP/DP/EXP/SUR
The relation of Degrees Baumb or h.P.1. to Specific Grawry IJ expressed by the following formulas: For liguds
lighter than water:
Degrees Baumk = -!$- - 130. G=
140
130 + Degrees Baumi
Degrees A.P.I. = y C= For lrqolds
heavier
- 131.5.
141.5 131.5 + Degrees A.P.I.
than
‘C = ‘F = K= “R =
water:
Degrees Eauma = 145 - F.
C=
145
145 - Degrees BaumC SI Rcftxa
G = Specific Gravity = ratio of the weight of a given volume of oil at 60” Fahrenheit to the weight of the same volume of water et 60” Fahrenheir To determine the resulting ferent gravltla: D=
gravity
USEFUL NON
Accduaum I
IO”
by mixing oils of dif-
of grrviry
Gravity of oil of of oil of denrity density
of mixture dl density dz denrity of m oil of n oil
Fsctm
symtd
Pm
a
IP
%?
k
M
hato dea dai centi milli miau ran0
h dr d al u 0
ZiO ItlO
; I
C
j
MASSE
:. I
qnmmc 8. . mmc
1 ne mCtnqu
I
= 9.61 mfr2 32.17 tr/d
l d Multipliarfm
Rda terr
JO’ IV
10’ IO’ IO10-a IO-’ IF IO-’ lo-” lo-” lo-‘*
mdt + ndz mtn
D = Density or Spktic m = Volume proportion n = Volume proponion dt = Specific Gravity or Q = Specific Gravity or
I
519 (“F - 32) 9/S (“C) + 32 “C + 273.15 = S/9 R “F + 459.67 - 1.8 K
I
I
nton
IUJ
001bm) -I-g Ion IL f3 ‘40 Ibm)
/
roTAL
PROCESS ENGINEERING DATA
DESiGN MANUAL
SECTION
Revision
:
0
Date
: 2/85
P8g8
15 -
No :
3
MASS son (short1
.OOO CXX EMI3
2.834
952
E-02
wm9l
1,000
000
E-03
2.2O4
622
E+OO
3.527
397
E to1
~ .102311
E-03
9.842064
E-O4
l.OOO
OOO E-06
2.204
622
E -03
3.527
397
E -02
.102311
E-O6
9.842064
E-07
2.204
622
E ~33
3.527
397
E+O4
I.102311
EMO
9.842064
E-01
1.600
000
E +Ol
5.000
1
.OOOOOOE+06
1 ocx3000E+03
ton
I I 1
I.535
924
E +Q2
4.5?5
924
E -04
1
2.834
952
E +Ol
2.834
952
E-M
6.2SO
9.071
647E-01
OMJ E -04
4.464
286
E-Or
1
3.12SOOOE-05
2.790
178E-O!
2.OOOOOUEfo3
3.200OOOE+04
I
a.928
570
2.240OOOE+O3
3,584C0OE+O4
l.ImmoE+oo
1
00
E -02
I n ton
IUS.)
00 lbml
9.071
&(7
E+oI
3.071
847E+OS
'"'q Ion It .8.) ‘40 --I--
Ibml
l.O16Op7E+O3
l.o16047E+06
l.O16047E+OO
E -0
4 :’ .
TOTAL
PROCESS
r
ENGINEERING :
DESIGN
DATA SECXON
TEP/DP/EXP!SUR
0
Revision
:
Date
: 2/85
MANUAL
Page No :
15 -
4
L o4RE.4
CCnllmttRorrC
1.000000E-04
II
I
2.471 054 i-08
'.ooooooi-06
j
‘.55ow3E-01
j
!
art
‘.ooo000E+o2
I Icn
4.046856E+03
/ 2.4 71 on
’
4.~60%E+o7
4.046856E+Ol
cqurrt
tnch
6.451
600 E -04
6.4511 600 EM0
6.451
rlprrt
toor
9.290
304 E -02
9.290
9.290
304 E co2
1
EG
600
1.5%
LENGTH u
tnllmttre
1.omocaE-02
1
1.0000ooE-06
l.OOOOOOE-O*
~cptrom Ich (pow)
fCJOC (pttd)
E-05
E”03
4.3%
I
1
I.440
oca E+O2
6.944
3g’
000 E foe 1 I
444 E -03
1
-1
e
I
- .tn :“I
A
fC111
,
mtlt !I
I
II Lin c LL I-
cm
nr1rt
.Imeron I
22s E -07
‘.o76
0
m
m
I’
1.550003E-05 6,272639E+05
2.2%6&o
304 E-w
t LONGIJEUR
E -02
E-03
!
!
i
l.OOooOOEG
’ 076391
‘.000000E-IO
I.OOOOOOE-08
I
l.OWoOOE+06
l.M)OOOOE+10
3.937OO8E+ol
3.280840E+00
6.213712Eeo4;
‘.O@JO@JEW
‘.OOOOOOEW8
3.937008E-O’
3.28084OE-02
6.213
1
l.oOooOoE+04
3.937oOSE-05
3.280840E-06
6.213712E-10
I
, l.OOOWOE-or
1
3.937008E-09
3.280&40E-10
6.213
712E-14 -
2.YOOOO
E-02
2.54OOOQ
E+Oo
2540000E+CM
t.SoOOOOE+o0
1
8.33J
3.048OOOE+oS
3,0a8OOOE+o9
1.200OoOEWl
1
1.609344
1.609344
333 E-02
I -
1.578 283 E-05
M
.‘I 3,O480OOE+01
3B48000E-01
ldt (U.S. SCJ~IJC~) 1.609344
1.893 939 E-04
kil0g -
EM3
1,609
344 E+oS
Ei09
E+13
6.336OOoEW4
5.28ooOO
E+03
1
I pm
VELOCITY
I
pour P”’ PO”1 -
. -
i
I
TOTAL
PROCESS ENGINEERING DESIGN MANUAL
I------
DATA
TEP.‘DP/EXP/SUR
SZCTION
Revision : 0
’ .’ Date _.
: 2/85
-I
VOLUMETRIC
FLOW
-I
m’lmn
wm
ilSIS
*
tl’/h
Bblld
’ i
1.104
on
E-01
DENSITY MaSSE
VOLUMlaUE
m“ kg
mund
wr wb~c fco1
hdm
dcm
’
s
Ibh’
Iid
1.601 646 EW1
1.601 &(6 E-02
5.787
037 E-04
1
1.19B X4
1.1s
E-01
4.329
0011 E-03
7.460~19E+CG
II EM2
aj4
1.336 806 E-01
.
1
II
TOTAL TEP/DP/EXP/SUR
-yzr-jq; PROCESS ENGINEERING
DESlGN MANUAL
.i PRESSiRE
.
TOTAL
I PROCESS ENGINEERING DESIGN MANUAL .y” - DATA
TE?/DP/EXP/SUR
SECTION
VISCOSITY
jCOSlTE
I Revision : 0 Date
1 : Page No
: 2/85
(Kinematic) .
CINEh4ATIOUEI m’l,
CSI
11=.1,
tr:/ll
DIFFUSIVITE ml=
6
‘I
L‘
1
rntinok#r
l.ooooooEc06
1
1.OGoOooE-06 I
,uarr foot prr vcond
9.290304
uare fool per hour
2.580
E-02
1.076
391
E+Ol
1.076
391
E-05
I
9.290
300
E +cM
3.a75co8 E 44 3.875
ma
E -32
3.600
OW
E 43
I
1
,C-01
640
E -05
2.560
640
E +Ol
2.777
778
E -04
1
I-01
B’“I.T.hph -T-
.365666t-0,
1,556565t-0
TOTAL
PROCESS ENGlNEERtNG DATA
TEP/DP/EXP/SUR
DESIGN
MANUAL
SECTION
Date
: 2/85
15 - 8
i w
SPECIFIC
HEAT
I
CAPACITY
c
! THERhlAL
HEAT
CONDUCTIVITY
TRANSFER
COEFFICIENT
Brtrnh ptr de1
Tom& 1
PROCESS ENGlNEERlNG DATA
TEP/DP/EXP/SUR
DESIGN MANUAL
SZCTION
Revision
:
0
Date
: 2/8S
Page NO :
15 -
9
HEAT CAPACITY/ENTROPY
I
ENrROPlEl CAPACITE THERMIQUE
m:
cy.,
l&d/K
J/K
-z
.
I i
BCd- F
I
K-l
it I
2.390 05’1 E-W
i
1.706
071
E-03
7.138
2ooi-00
I I
.i.lW WOE+03
1
5.861422
l.ao
j I
I
t of rrfriq.
I I I I .’ I
I
I
POWER/HEATFLOWRATE
I
!
913 E-01
,.
t
I
EMI
’ *,mr
,w.u
.“,,
I.”
15,665,f”O
TOTAL
. .
..-
PROCESS
ENGINEERING
DESIGN
MANUAL
DATA SECTION
TEP/DP/EXP/SUR
Revision
:
Date
: 2/8S
r
0
Page No :
PSEUDO-CRITICALS
TEP
'5 -I()
I
-
AND OIL PROPERTIES h
1 Mer
True
vapour
temperature
prwure
: - actual
vapour
pressure
of a crude
oil
at the actual
of the fluid.
2 3 A 5
E:n Pro n-9 Irot
6
~J=I lsoc kc .1-H 24.4 3.4 Net 2.3.
c7
Reid
vapour
temperature
pressure
:
reference
-
vapour
pressure
of an oil
af a controlled
of 100 “F (used as a basis for product specification). ..
Molal
boiling
average
point
component x its atmospheric Volume average
: - equal boiling
point
boiiing
to the sum of the mole fracrion
point “R,
: VABP : - average
10 %, 30 %, 50 %, 70 % and 90 % volumes boil.
Mean
average
ro correct
kding
temperature
,
of each
af which the ASTM
22 23
no Our Isoc
VABP = TIO % + T30 % + T50 % + T70 % + T90 % 5
25 26 27 28 29 30
n-N, n.Dr Crc Mer’ Cvc Mer
: MABP : - the slope of the ASTIM distillation
31 32 33 34 y
Erht Proc 1-h err-; .-an mb
point
: CABP : - another
UOP K or WATSON CHARACTEFUSAIION K = CABP %
19 20 21
n-n 2M 344 3-51 22. 2.4. 33. Tnc
24
point
boiling
10 15 16 17 18
-
curve is used
the VABP to give MABP. See Fig. 7
Cubic average
J 11 12 13
‘4
corrected
form of VABP.
FACTOR sg at 60/60 CABP in “R
.
This issued as a characterisation various other data evaluations.
factor
when defining
crude oils. It is required
for
-.
--”
s5
-
TOlTib
PROCESS ENGINEERING Q.ESIGN MANUAL
TEP/D?/EXP/SUR
CONSTANTS
PHYSICAL
-I== SreNottNo
-
Page No :
OF HYOROCARBONS(27)
;
2.
1
Commund
2 3 0 5
16.O43 30.070 ~.W? 58.124 58.124
EvtJnt Prooanc n.&Jtsnt IrocwrJnc
-161.52(2E -88.58 -42.07 -0.49 -11.81
:5 ow.1 6000.b 1341. 377. 528.
12.151 72.151 72.151
EE 9.50
86.170 86.178 86.178 86.118 86.178
68.74 60.26 63.27 49.73 57.98
:3::: 55.34
loo.205 100.2O5 im.205 im.205 I 00.205 too.205 too.205 i m.205
98.42 90.05 91.85 93.48 79.19 80.49 86.06 80.88
1230 1722 16.16 15.27 26.32 24.04 2093 25.40
it E
I14232 114232 !14.232 128.259 142286 70.135 84.162 84.162 96.189
125.67 103.11 9924 150.82 174.16 49.25 71.81 80.73 loo.93
% 33 34 F
Z&O54 42.oBl 56.108 56.lO6 56.108
-103.77m -47.72 -6.23 3.72
4.143 8.417 12.96 1.40 0.473: 73.91 33.85 24.63 12.213 -
::
16 17 18 :: 21 z! 23 I: f ':
Jlj 3Q
1PJnIJm 13&JIJolene 138UI~lJne
40
IsoofCM
Exz 54.092 22% A 26.038 78.114 92.141 106.168 106.166 106.166 106.168 104.152 lM.195
ACIWICM
41
62
Bcnzcrr
43 44 45 46 47 46 t I 49 50 I
Tolucne Etnvlbtnrcnc o.xvlcnc m.xvh?nJ LB-Xvlcne Swmt lSOO~OOYItlCI-lltN
51 52 53 54 55
Mtlnvl ElhVl CJrWn
Jlconol JkOnOl monoxmx Groan OIORKIC ~v0eqtn wlftae Sulfw at0~m
56 57 58 55 ISO 61
Ammoma AM Hrdrcqtn O.vpen Nttr~pen Cnwlnt WJ1.r
63 64
Utlwm
62
uvdmqtn
.
-.--
cnmrtat
-
- .
ZU.0
C~H,O :0
-!gY 2946 10.85 -4.41 36.07 -84.8@ 80.09 110.63 136.20 144.43 139.12
:z::
32.O42 46.069 28.010 44.010 34.076 64059
152:41 649 70.29 -19149 -xl.51* -60.31 -10.02
17031 28.9W 2.016 31.999 28.013 70.906 18.015 am3 36461
-33.33(x1 -194.2121 -252.87" - 182.962" -195.80(31 -a.03 100.00” -268.93(32 -65.00 ---.
-182.4?* -182EO4 -187.684 -138.36 -159.60
115.66 151.3 289. 3728 50.68
1596: 451.9 337.6 365.8 452.3 141.65 269. 43a. 12377 2436 7 895 2.07 2.05 253 2.65 185 1.47 36.43 17.70
-
2881. 6X.8 1513. A -
-95.32 -153.66 -99870 -128.54 -90.582 -llE2? -118.6O -123.81 -119.24 "%3:, A -56.76 -91200 -107‘36 -53.49 -29.64 -93.866 -142.46 6.554 -126.59 -169.1S4 -18525d 45;:" -105.55 -140.35 - .--165.22 -136.19 -108.91 -145.95 -8O.ed 5.533 -94 99 1 -94975 -25.18~ 47.87 13.26 -30.61 -96.035 -97.68 -114
1
-2Q5.04 -56.574 -85.534 -75.484 --77.d
.
190.55 305.43 369.82 425.16 406 13
o.w6 17 O.OO492 o.ocd 6.0 o.w4 33 0.004 52
3368. 3361. 3199.
469.6 460.39 433.75
0.004 21 O.ooO 24 0.004 20
3012. 3010. 3 124.
5074 497.45 sm.4 400.73 499.93
0.004 29 0.03426 0.001126 o.oDa17 0.004 15
540.2 530.31 535.13 p,::z '519.73 536.36 531 11
o.OO431 0.0% 20 o.OO403 o.oDp 15 0.004 15 o.ooo 17 o.ooo 13 0.003 97
568.76 599.99 543.89 594.56 617.4 511.6 532.73 553.5 572.12
o.ma 0.004 o.ma 0.004 O.ooO 0.003 0.063 0.003 0.003
31 22 10 27 24 71 79 68 75
282.35 3m.85 419.53 435.56 426.63 417.90 4M.78 lM4.1 425. '4&d .I
O.ooO 0.004 0.004 0.004 O.tXX O.OCM o.ca IO.009 o.ooa (0.004
67 30 28 17 24 26 22 05) 09 061
5061. 3127
2736. 27w. 2814. 2891. 2773. 2 137. 2945. 2954. 2- 486. --. 2486. f Z: 2099. 4 5O2. 3 785. 4 074. 3472. 5001. 4 600. 4 023. 4 220. 4-07
E:
(4 5O2.1 4 330. 13850.) 6139. 4896. 4 106.
3609. 3734. 3536. 3511. 3999. 3209. 8096. 6 383. 3 4QQ.u3) 7 382.m) 9m5. 7 894.
11260. 3 771.12) 1299) 5081. 3399. 7711
113J 7377
22 118. 227.5n2I -0303.- ._- .-._
ma.33 562.16 591.80 617.20 6P.33 611.05 616.23 6476 631.1
o.ow 34 0.00328 o.m3 43 0.033 53 0.003 46 0.00346 0.003 54 0.00354 0.00356 0.003 38 0.00357
512.W 513.92 132.9213: 300 19(X 373.5 430.6
0.003 6a 0.0036a 0.00362 62 0.003 0.003 x2(331 32(331 0.002 o.OcJ2 14l33) 14133) 0.002 07
405.6 132 412) 33.2 154 71331 126.1 417 6473 5.2(321 324 7-- ..._-_
O.OrJl 0.00190 90
0.001 0.003 0014 _o.w222
75 18 36(321
.
PROCESS ENGINEEEICS
SECTION
DATA
TEP/DP/EXP/SUR
Date
I PHYSICAL
Revision :
DESIGN MANUAL
CONSTANTS
: z/es
OF HYDROCARBONSl27)
I
I -: -I -z+= g4
0.3)’ 03581h O.SC& 05!347.0.5637"
l3w.)' 357.P.
0.6316
631.0 624.4 596. 7h
629.9 623.3 595.6'
0.6644 0.6583 0.6694 0.6545 06668
6633 657.7 6688 653.9 666.2
0 6686 0.6635 0.6921 0.7032 0.6787 0.6777 0.6980 0.6950
$$' 563.2'
300.1' 356.6' 506.7' 583.1' 562.1'
CLOSI’ 0.08404” 0.00684h 0.099ah 0.103 t4
0 .WT?dh 0.002 0.002
llrn lQh
0.0126 0.0978 0.1541 0.2015 O.lsao
0.998I 0.9915 0.9810 0.9m1 0.9665
1.0382 1.5225
;:z
0.001 57 0.00162 0.W16?h
0.252* 02286 0.1967
0.9421 0.908t 0.9538
Z.ogrc
662.7 656.6 667.7 652.8 665.1
zsii 0.2704 0.2741 02333 0.2475
0.9107
2.9753
0.131 0.129
O.Wl 35 O.Wlag 0.001 3s O.Wl40 o.w13!5
688.0 662.8 691.5 702.6 676.0 677.1 697.4 694.4
686.9 681.7 690.4 701.5 676.9 676.0 696.3 693.3
0.1456 0.146B 0.144 0.1426 0.147 0.148 0.143 0.144
0.001 24 O.Wl22 O.Wl 24 0.001 26
0.8521
0.7073 0.6984 0.6966 0.7224 0.7346 0.7508 0.7511 0.7836 0.7744
706.7 697.7 6s6.0 721.7 733.9 750.2 753.4 783.1 773.7
705.6 696.6 694.9 720.6 732.8 749.1 752.3 782.0 772.6
0.161 0.163 0.164 0.177 0.1939 009349 0.111 0.107 0.126
0.783t
0.5231h 06019h 0.6277h 0.610Sh 0.6clOh 06462 0.6576h 0.626d 0.6866
522.6”*’
521.5' 6ocl.j 626.d 608.9' 599.4"
0.675' o.aixci 08723 00721 0 8850 0.6691 0.6661 0.9115
601 4h 627.1h 610.0h 600.Sh 645.f 657. 627.0h 686.0
-
3 626:y 684.9 -
884 2 6716 671 3 880.2 868.3 865.3 910.6 866.0
883.1 870.5 070.5 883.1 067.2 864.2 909.5 aw.9
796.0 791.5 768.6"(341 821.9hms, 789~.'(36 396. .'f361
19r1.9 790.4
617 +(fO, ess.71.oom(371
616.6"
iai.mfja)
aO8.6"'(331~ 4245 9991 ~25.U-'(321 053ti
8 4
0 7 3
i%E o:w1 O-Ml
ii 17 24
0.3494 0.3x3 0.3239 0.3107 02876 0.3o31 02631 0.2509
6 7 1 7
O.ool 12 0.001 17 0.001 17 0.001 I3 o.wo 99 0.001 26 0.001 28 0.00122 O.ool 13
0481 0.3564 0.3o41 0.4452 a.49@ 0.1945 0.2308 0.2038 0.2364
9
a
7 5 9 h
::Ei 53 0.08947" 0.0919P 0.09300h 0.108 6 p3&3$ 3.099
30
o.c33
34
0.10" 0.121 0.120 0.122 0.122 0.114 0.139
7 9 i
3 7 4 0
020.0" 787.24 395.
423.5 998.0 6519
0.0339" 0.028 39" 0.02a o4m 0.034 wm 0.049 76 0.01803 0.032020.042 74
o.GM 0.00209"
0.001 76& O.WlO~
0.W2 16h
0.0869 0.1443 0.1949 0.2033 0.2126 0.2026 0.2334 0.2s40 0.1971 0.1567
2.4911 2.a9r I
0.7862 0.5362 o.afxa 0.4068
s.os96 3.45% 3.4596 3.45%
-
E$ 3.45% 7.4596
0.949t -
2
0.3277 0.3277
s 0.9938
0.9844 0.9703 0.9660 0.9661 0.9608 0.9ar IO.9591 IO.9651 0.949t
0.001 60 0.001 76h o.w2oY O.WlS5 0.001 19 O.Wloa o.wo 97 o.ow 99 o.oou 97 o.ow 97 o.oo103 o.wo 97
0.r893 0.2095 0.2633 0.3031 0.3113 0.3257 0.3214 0.1997 0.3260
0.9925 0.92+ 0.903' -
cl.Wl 17 o.oo107 -
0.5608 0.6608 On442 0.2667 0.0920 0.2546
o.ooo 0.006
14
0.2976 0/19w .-I.0200 0.0372 0.0737 0.3434
03
00.1232
0.2360 0.236o 0236o 0.2360 0.2360 0.2m 02360 02360
39439 3.9439 39439 -.- -_ 4.4282 4.9125
19372 19372 19372 ::2: 18676 2.3519
0.5619 0.4214 0.4214 0.4214 0.4214 0.3371 0.4371 0.4371 0.3471 0.9061 0.3027
-
1.1063
0.7379
09995
:*9z I:5195 1.1765 22117
05122 0.64~ I 0.5373 0.6939 0.3691
0.9943 0.99o3 0.9aott
0.9899(301 0.5880 0.99% 1.ooaJ l.WO6 O.oa% 0.9993(391 0.9997 :0.9875)'06!
1.wo 5l-m -
-
%
-EC 1 706 1625 1.652 1616
206.8 204.6 195.5'
1.622 1.600 1.624
w
182.1 180.5 183.5 179.4 182.6
TX5 I.602 1.578 1.593 1.566
2.231 2.205 2.170 2.148 2.146
162.4 161.1 163,2 165.8
1.606 1.595 1.564 1.613 1.613 1.651 1.603 1.578
2109 2.183 2.137 2.150 2.161 2.193 2.099 2.088
Tizi 1.573 1.599 1.590 1 s95 1.133 1.258 1211 1.324 -1.514 1.480 1.483 1.366 1.528 1.547 1.519 1.446 I.426 1.492
2.191 2.138 2.oa9 2.164 2.179 1.763 1.843 1.811 1.839 2.443 2.237 2.24lf 2.23a 2.296 2.241f43 2.262 2.124 2.171 -
;Ei:: 164.6 163.9 lrg.3 144.4 144.1 133.0 122.0 2s2.9 211.7 220.0 186.3 293.6' 253.4' 264.9 257.1' 253.1' 217.7 207.2 274.2 238.1 2676 223.7 194.0 196.9 193.4 192.7 206.7 170.4
o.&a2g
.--.-
o.esso 2.6989 3.1812 3.6655 3.6655 3.6655 3.66% 359% 4.14%
-
LOAl
i442.1' 231.3 272.3
f-;:g 29753 29753
-
oea1 ga:
1.1008 O.%R 2.4481 0.6220 0.1362 I2566
1.388 0.8163 1.73 0.7389 OE441 0.3335 1.312 5907 0.645 v-w-
v E
*4
P,
0.5539 i 374
iillS 0.120sh
0.1103
0
xi77 406.2 441.6A E-57.5& 5lS.Y a574 075.0 1311. 553.2
1.659 1.014 1.085 1.169 .I.218 1.163 1.157 1.133 1.219
I"
5 I’S
3807
2.076 2.366(41 2.366141
2.317
: :::51.721 1.741 1.696 1.708 1.724 1.732
Tz? 1.389 t 040 0.63X 0.996( 0.606;
2.rSd 2.340 2.o806l 1.3!59(36
2.019 1005 la.20 0.916e 1000 0476C I a62 5.192 0 799
469X30 L 4 191 -
1 1,. 18
..2 13
;: 2
14 1s 16 I? 18 19 20 i 2\
n 2 3 3 2 2 3 -f
:P 2 5 23 I 2' 2 2 I 2
20,.
,
3 5 3: i' i 34
i 42 43 4 4 4 47' 40
a’ 5 5
56 57 58 59 60 61 62 63 64
I 1 k ( r ( i ) b
I
I Revision : 0
PROCESS ENGINEERING DESIGN MANUAL
Page No :
I DATA
TEP/DF/EXP/SUR PHYSICAL
SECTION
CONSTANTS
Date
: 2/85
I5 -
OF HYDROCARBONS(27)
-;; =5ss ; 2 2 CC
?I t
;
3
.uernanc f mane prooane
33.936 60.395 66.456 112.384 112.031
tt-ab.nt
18ow 25394' 287lV 27621'
lA8.739
1 48.427
3.Echvlantme
190.327
22.bne?hvlmnIane
2 A.Dtmecnvtpenranc 3.3-~l~IhvlOWtWe
189.6M 189.803 189.885 169.690
nOzIanc o~lsoeuIvl ISOOCIJfW n-Nonane n-Deane CvcloDencrm Mecnvlcyc*orxnrane Cvclohexrne MelhvltyclohexAne
216.374 215.797 215.732 242.398 268.36 131.114 156.757 156.03A 181.567
233286 232.709 232.6AA 261.109 289.066 1~0.so9 168.032 167.308 194.720
47.919 47.832 47.843 47.703 47.670 46955 46.025 46.606 46.525
55.942 81.482
59.700 07.119 114.991 114.707 114.473 116271 142.860 109.755 107.555 134846
a.081 47.927 47.843 47.769 47.788 47.5w 46.608 46.406
3-Merhvlherrne
Emene
(Erwkne)
ProoenelProovlenel l-htene IButylme~ 02.24utene rrwlr-2&cem
107.455 107.191 106.957 106.755 133.465
IsoouIcne -Pcotcne * .2.BuIaelcn 1.3-Bu1~01ene lsOOrme
104.118
101.917 127.330
a2 A3
To~ucne EInvleanzcm 0.XVlCl-W m.Xv1et-e
j ,
o.xvlcne
I
Stvrene Isooroovlbenzene
Q .’ A? rg A’
Metnvl Elnvl
Groan
Gmon OIOXIO~ +araren SUI~I~C
60 61 62 63 64
N*rropcn Ch~orme Wafer +twm HvarCgen
-I-
cn~or~~~
gg: 33488 33319
294.41
u 33372 33299 3448S 34985
30126 285.69 271.04 288.82 276X)6 38920 345.51 35595 317.03
%ffZ 36A97 35997
26916, 30055 29lW boil' 312104 29242' 31836
36998 37 ow 37470 3793s 37 24s 37 122 38439 37591 16057 23513
10.230 -m -m 0---
““( 12.091
-z79
0 -
97 I 89.V 976
1.3A5
:2z
38.18 38.18 39.18
1.4 1 .A 1.6
ifs7 90.3 80.2
61.)' 92.3 05.5
137746 137417 1.379 18 1.37157 1337759
rg.ja 453 45.34 45.34 45.3
26.0 73.5 'Ia. 93.A 90.3
24.8 73A 74 5 91.6 9.3f
0.0 46.4 55.6 69.3 95.6 638 86.6 4.d
0.0 42.4 52.0 65.0 92.6 83.1 80.8
52.50 52.50 ~~~ 52150 52.50 ~Z
288.90
4a2.77 43x68 390.60 016.10 40556 35925 M-49.6) (418.7) 1385.21
1.39981 1.39r06 1.39392 l.AO773 1.414 11 1.40927 1.41240 1.42892 1.425 66
83.32 360.14 33498 346.80 32.47
333.92 (35123) 31225 iO7597 BUO.SU 215.70 573.27" SA8.01 1366.
-
214. 4504 213. 2oa 288.0 2257 A31.5
59.65 E:E 66.81 7397 '35.79 42.95 42.95
-
1.374 ,-
61
1.42s
36
26.25 26.25 33.41
1.50032 1.49973 1.498 56 1.5079s 1.099 80 1.090 39 1.54969 1.494 00
Fz 35.79 4295 50.11 50.11 50.11 50.11 al.72 57.27
1.330 20 1.363AS Loo0 36 1.00049 1.00061 1.0CC162 l.aKl36 l.ooo13 l.a302? l.MX)28 ,m,er 1.33347 l.oooO3 l.oooA2
1.16 14.32 2.39 7.16
3.58 -
+ I .p.: . I .w.' ::. Yd.
l 1B
096
IO981 G7J 0.W (1.4) (121 I.3 12
'E r1b 2.5 1.Y 1.F FY 1.1‘ 1.1' 1.1 0.08' 6.?2(51 3.26tSI 12.50~sI
4.300(51 15.MlSl
2.39 -
-.05
1 .o 11.01 t1.01 (1.01 (1.01 (1.01 Il.01 (1.01,
2.7 2.0 1.6 (1.6) (1.61 (1.61 1.4
-
-
-
0 -
2.9 2.1 l.E IS
295.87
387.74
--
t6.70 2386 31.02 31.02
%S 308.9A 291.03
394.18
2Y.912
17 301
nmmmoJ A,,
uo95 32809 33249 33 796
28.M)1 56.062 11.959
.lEOrlOl JICOhOf mono.aae
5.3
316.33
48.10o aos1 A8.082 08.101 47960 ag.wo 08.019 A7982
u.098 13A.055 ls9.53n 185.S55 185.092 185.020 1850s 180.290 211.328
~~~vleoc Benzene
a a
r:E 321s7 205.431 205132 205.276 205.359 20A.662 204.836 204918 200.722
130.398 190.099 190.243
2-Mccnvrhex4ne
I
'35722 34220 315.30
3203r 31 749
I U.402 164.075 164.188 163.683 16A.025 n-+hXHJnC
Eisj
9.5a
509.86 489.36 425.73 38526 366.40
3Q709 137.A6S
13
4 OOIS) -
-
2.9. 2.6 8.35 7.8
55.7 00. 84s'
+0.d 91 3
E;o
83.0 74.0
71
3=r
10.0 9.3 -
-
0.7 (12.1 11.5
.l
15.6
7 l 0.0
'3 83.5 -. 77.1
9:: 100.
81.0 80. 7.9’ 7.11 6.?' I ,"a8 6.6' 6.1 6.5'
l 2.d +0.3/ 97.9 loo. *2.6' -1.2' -0.2' 99'3
36.50 AS.%
90.9 99 1
lI5.a 9.8’ l A d
l 3. f 4
*3.
l 2 1'
-
-
-
-
16.95 74.20
27w 7420 -
7
PROCESS E’NGINEEA,ING
TOTAL
DATA
TEP/DP/EXP/SUR
i351 ml
cm 133 139) I401 (411 c42l 1431
SECTION
Hwt. J. C.. Scr-wt. R 0. ‘+llwnwdyn.mu Row* V.1u.q for G.J.w. .nd Lsqwd C.rbon Mono.:de from 70 w ja, K -,,h Rnwm (0 300 A~maghertc.Vac. Bw:Stmd. U.S. Tech. a%tr No 202 Yorwnbtr 30. 1% hm;. 5.; Anmcmne. 8.: dc fbuck. K M.. Ed.. “Cubon Dm.,d.. In~rrn~oon~l Thtrmodrnmmtc T3bl.a of ch. fled SU,r3’. Ptrc.mon Rn.: O.ford. 19%. ‘Thhr ,M.,hwn Un.bndr.d C.. Dqu Brisk’: .U.ch..on 6. Rducu: NcYork. 1974. Dean. J. W. ‘A T.bul.uon of rhr Thcrmcdrn.mic Roprur of .Normd Hydrown fpm IaTrmpn.,um LO 300 K qnd from I 10 100 Atmo.vn.rn . Sat. Rur. Stand. US. 1-h. NOW 30. 120. N~.tmlmr 1951 .UcC.ny. R D.: We&r. L A. 7bmrmophy.ic~ Row.. of OxyKm front th. Frcr.,n6 Lnc to bQc*R for Re..um u) .WOV P.I.“. N.r. 8~. Stand. US. Tech .%rr No. 364. July 1971. WM. L A. Nat. Bur. Stand. U.S. Rrm No. S710. I%& lhdnbtrr. N.~ v.. PO /WY V. N., Siorotow~.N~A. T?wrmodyn.m‘c .nd Thtrmo hy.aa F’wmtn~t. of H~lwn : Atoma.ac Moue-. ‘mama for sclcnok lhnd.1lon. 1971. I%* I.r.4 Toulouk:.o. Y. S.. .Sldt~U. T. ‘~ermophr.w.1 Row’U~ of S4.tt.r. Vol. 6. SvtctBc Hrac. ?lon.mrtcrll~ bus& .nd G...s-: lFl/PI*nurn: ?I*York. 19io. Schbnrrr. W G.: 5.~. 8. H. lad. EM. Chrn. IS5L 44. 24% Todd. 5. S.: Olircr. C. 0.: Huffm.n. P. M. d. Am. Chum. Ser. IS47. 63. ISIS.
NOTES . b c
d t f
AM .m~r.ud liowd. Abwluu rJw. from -ewhu an “.cuY~. llw .vv.rw“ rduw (mm weash, ‘n .I, .n .horn 61 uun’ con. vcrwncc .nd comphanrr -ah ASTXIP Petmlman Mcvurcmml Tabln. In ,h. Un,,rd S,.,.. .nd Cm, Bn,.m. .II comm.rn.l -etsh,. .r. reqwred by I.u, b. -aqhu an .,I. All olher m.” d.u .r. on .n l bwluw m... I-&h& ,n ..cuum# b..,.. AI ..‘“,.“a” vr”.ur, Imvl, vmnt,. Subhmwon p.an~
c h
S.‘ur.uon Avv.ttnl
vr”.un vduc .I
.nd WC.
IS-C.
OESIGN MANUAL
Revision
:
0
Date
: 2/85
Page No :
IS
-14
PROCESS
ENGINEERING
DSS~GN
DATA SECTION
TEP/CP/EXP/SUR
MANUAL
Revision
:
0
Date
: z/es
Page No :
15 - 15
I
COlcllPRESSIBILITY FOR NATURAL
,
3-rk-Y. :1.. _ :.:-I.. I-::.,, .:.
:. -_~ . . . . . . . .. . . . . . . __ i..!..
: . ._ . .:
:_
. -y -.... i:
.-.. :
1
1..-. \ ,
.--.
..:.:. . . . ~. . . .. .. .. . ... . . . .A.:-_......... ,“‘..“”
~~~~~~~~~~~~::.“.F.
::
.
l./+.’ i . _,. . ... .. :
1 .::;;:..;x:-;
: ‘I :,iy-
. .
:
.
.: : ...... -1..:::::. .:.:;:;.1.:“““‘ , . .1.-;-.-..--~.--i--:. : : . . . . . . ..I.........~... e1E.,:, --“.i.,A ;i, .:. ....-............... _.. .. ._. : : ! ...................-... .i i: i.... . . . .. .. ...--.._.__._......... .. :’. I:::‘::: :: . I-_,... .. ..fiI:fii^iii~~~i~~:~*~:=~ .. .; . . ! . . . . . . . ..-.m__......_..... . . . . . . . .
.-:... i
I.
.--.
.x’
g-.*; II
FACTORS GAS
PROCESS ENGINEERING DATA
TEP/DP/EXP/SUR
Revision :
DESIGN MANUAL
I
SECTION
I
Date
0
Page No :
: 2/85
I
SJOO
J500
mul
uxa
3500
loo0
2x0 10
10
JO
so-
40 *blrcJa-
60
70
80
90
loo
is - 16
TEPID
1
1
Revision :
PROCESS ENGINEERING DESIGN MANUAL DATA
-rEP/D?/EXP/SLJR
SECTION
Dare
~. . . . .. .: .:, . . . .. .. y..; . . &
*reraae
6.P -iloesr
ALL-
:: .:...
,
:... ‘::.. 1 . .
. !.
:..:.. L; ! . “, ,:..,,.::... J.1 1. .,....: .’ I . . . . . . :::’ .:.
I
! :;.;-I j
: !
i
i’,‘if’:
: :i !,
i :
.i-
I.:.,;
--
I
;
i
Page NO :
: 2/85
I5
-
I7
i .-Ii.../ ;
.“j
0
i
i.. . !.._ i. !:::.;.. i I o.wJ ‘0.850 1 .‘rYfY .,. .--_f i ;J$7zy 0.8~~ :
280 260 240 : .:.:y:,::
i::::
‘.:i. --m-a.:l:.::L:::. ::i .I :: : :-:i.-;;: :. .:::.
,.:.:i.
1 ::
i 220 , :’ 1’: 1
.I:-:.. .I
:::,.::: 1::::: ::.i:::::.:+::i .. .. .
,:: . . _.: ~.,I::iii:t!il.:.~i::1:1 ___:,.... ,...:; . . ..I. :..:..
.
:::i .:.:.
: 1 6oo :
580
300
400 Norm01
boiling
p&m.
‘C
500
PROCESS ENGINEE~IhjG
DESIGN MANUAL
Revision
:
0
Page No :
’ .
DATA
TEP/DP/EXP/SUR
SECTION
Date
: 2/85
1
IS
-18
1
I VAPC I t Vapor I
I
I
I I
ecular mass, boiling nd relative densities
’
p fo
LlQUl I The
I
)ata (
,..
. . .. . .
)-..:
I.....,:,
6OOkon
200
100
Mean
average
boiling
Hvdrocarbons" --
.._‘~
,
point.
,_
,
,
%-In -.--
oC
’ i
,
~ ,
~ .._:: a..::
’
llnn -vv
liquid
d
-‘.“-
PROCESS ENGINEERING DhTk
TEP/DP/EXP/SUR
S&C-X
DESIGN MANUAL
Revision : 0
ON
Date
: 2785
-
Page No :
‘5-19
DENSITY 1 .
P
VAPOUR DENSITY
Vapour densities or molar volumes can be calculated
from the equation:
v _ -- ZRT P
I p
I
IP
- MW.P ZRT
T
L
Specific
pravity
of a gas
I
bara
I
I
‘K
I?. I
I I
I psia OR
10.73 1
I Ibs/ft3
I
0.08314 Kg/m3
=MWF: MWa.ir
MWair
= 28.967
I I I
LIQUID DENSITY The density --mponkt
-
of a multi densities
component
mixture
can be calculated
using the summation
of the
:
I
Wi = mass component pi = density component
I I I I I -
I
liquid densities for hydrocarbon
mixtures
can be estimated
using. Figures 10, 11 in this section.
TO’tBL-,
PROCESS Et .IINEERING DA-PA
TEP/DP/EXP/SUR
DESIGN MANUAL
SECTION
Revision
Date
:
0
TO
Page No :
: 2/85
15
-
20
*’ 1
Approximate
relative
density
of petroleum
fractions
FIG.
18
.’ !
~~lllli!lY~
0.3 0
20
40
$0
TEP/D;
PROCESS ENGINEERING DESIGN MANUAL
No :
DATA
TEP/D;/EXP/SUR
Relative
density
SECTION
Revision : 0 Date
of petroleum
: 2/85
fractions
Example: At 300°C
0;
an oil with rel. den. at IS’C and 101.325 kPa(absj of O.S6. and Kw 11.00; has a rei. den. of 0.636 at 7500 kPa(abs@).
KW =
[(Mean avg. B.P.. ‘C - 273.15) X 1.31”’ F&l. den. at 15°C and 101.325 kPa(abs)
0.85
\ \ \ 0.80
0.75
0.70
0.65
50
0.60
0.55 1 Oj
0.50 0 A5
Adopwd 10 $1 by GP’SA from Ptner. L.no,r. and kh-•pps. P.woleum Rsl~ner,
I958
Page No :
IS-21
_~-~ TUTAL
PROCESS ENGINEERING DATA
TEP/DP/EXP/SUR
DESIGN MAr:;iAL
SECTION
Date
: 2/85
‘Lz2
VISCOSITY UNITS : Dvnanlc Kinematic
vlscositv viscositv
:
1 centipose
=
0.01 dyne.sec/c.m2
:
I centistoke
=
C-01 cm2/s
Orner quoted units for kinematic
viscosity
=
.
Redwood
Saybolt furol
conversion
Calculate
’
_
charts are sited in literature I
12 in this section or using :
D?na~~~s;~;cositv
Engler
Saybolt universal
Use figure
0.000672 IbPmift set
are :
VAPOUR VISCOSITY .
=
pn
i)
ii)
-
=
&Iu: y: P/W-J; f
y;J-c-
mixture
.P= “p;
=
component
viscosity
’ rr\bl: =
component
mol.wt
3; = component mol.frac accuracy 2 5 %
p m y A exp (B/‘cl
7-h
C =
2.4
-
viscosity
lq
O-29
LIQUID VISCOSiTY .
Use Figure 13 in this section or : -
.
Calculate
.
The viscosity
using :
Correlations
component
mol.frac
of crude oils with an API > 30 o (sg = 0.88) can be estimated using : . iOg = a - (O.O35)(API) centipoise r a “C I
where
.
x; =
i)
for liquid viscosity
38
I
2.05
54 71 88 104
I I
1.83 1.55 1.30 1.08
possess a general
reliability
of 2 I5 %
1
No: ’
I
I
-
PROCESS ENGINEERING DESIGN MANUAL
POTAh
DATA
TEP/D?/EXP/SUR
SECTION
I
Revision :
Date
0
: 2/85
+
Tempemture. (b)
VlSCOSITY
OF NATURAL
GASES
dq F
7 Page NO :
l5 -23
PROCESS ENGINEERING TEP/DP/EXP/SUR
DATA SECTION
DESIGN MANUAL
Revision :
Date
0
: ~/ES
TEP/I
PROCESS ENGINE~,j?l~G TEP/DP/EXP/SUR
DESIGN MANUAL
DATA SZCTION !SOe)
sqe)
edy
‘CJJnsSaJd
lode/\
Revision
:
0
PROCESS ENGINEERING DATA
TEP/C?/EXP/SUR
tlJESlGN MANUAL .
SECTIOt-’
Revision
:
0
Date
: Z/85
. .
1 0.9
0.8
I.. ,,(_aI* o.sL’.,‘..:;;; I*
I..’ 0
. .
,
:.. ..I,
;
. . ..l J-1
;;;,s,,Ttx ,/
iI, ,., !,I, 100
200
. 300
temperature
40
OF
SW
600
700
t3cF
Page No :
‘5-25
C
TOTIlL TEP/DT’/EXP/SUR
PROCESS ENGINEERING DATA
SECTION
DESIGN MANUAL
Revision :
Date
0
: 2/85
PageNo :
‘5-27
PROCESS ENGINEERIKG
DESIGN
MANUAL
Revision
:
0
Date
: Z/ES
Page NO
I
DATA
TEP/DP/EXP/SUR
SECTION
I
FIG.
16
TRUE
VAPOUR
PRESSl‘?ES
OF PETROLEUM
I
PRODUCTS
AND
CRUDE
IS -2E 3
OIL
I
I
PROCESS ENGINEERING DES!GN MANUAL DATA
SECTION
TEP/lY/EXP/SUR
Revision
:
0
Date
: 2/85
Page No :
‘5
-29
Permissible expansion of a 0.6 relallve density
Permissible expansion of a 0.7 relalive density natural gas wlthout hydrate formation
.
7oco3 6OooO.”
;
;!I loo01 ’
2ooa
1000
3ooo so00 Final pressure.
lor pr.dMlng
hydde
2oooo
1OOW kPa (abs)
30(
Final presqurc kPa tabs)
Permitrlble natural
tomutlon
expansion of a 0.6 relatlvc density gas without hydrate formation
7ocm, .---6oooo
50000 : . ..l..:.j:;::1::::;:iiif:~iii:I:::i 4 . *. _. . .._ . . . . .
, ..,....,....I.. :... !._..I..
!Ocrm woo Urn -u J
.,../r
4OOW
.Y...
3oooo 2sooo 20000
:Jm 2
.-j:: .-
,- ---’ //I/i Es00 / Jcm*
!
: :
: I
#
:
i
! i.
i :
j ::
: t
;
.!..:;,:.!j.: !:...i
/
I
i
I’.IaI
!
:
;
i
;
i..
:
i
j:-:i::j .
.!
:
.-..
. -. . -
.
I
;
.;:.i
.I
1
/
. loal/ loo0
FIG.
17
HYDRATE
2Mx)
FORMATION
3ooo‘oal 6ooo 10000 Fmal pressure. kPa laos)
20000
-
PROCESS ENGINEER!NG :
OESICN MANUAL
DATA SECTION
TEP/DP/EXP/SUR
SPECIFIC
(HEAT
Revision
:
0
Date
: 2/85
’
Page NO : J5 -
30
i
HEATS e-
CAPACITY)
: I UNITS:
BTU/LB
“F
KJ/KC
“C
,I BTU/lb “F
=
4.19 KJ/Kg
I BTU/lb “F
=
1 Cal/g “C
‘C
VAPOUR MIXTURES .
Use figs 18, 19 in this iecfion
,
Cp” is a fuction
w
of temperature
and can be calculated
I’ ,
using’: .
Cp” = A + BT + CT2 where A, 8, C are constants
dependant on system composition
and T is in “R (K) Values of A, 8, C are cited in Kern, or Perry. Cp’ can be corrected .
K
=
ratio of specific
for pressure if Pr and Tr are known using Figure heats 9 this should also be corrected cv
for pressure if required. -_
LIQUID MIXTURES .
Use Figure 21
I
Calculate
in this section or :
using
CPl
=
2.96 - 1.34 C + T (0.00620
CPl
=
0.68 - 0.31 C + T (0.00082 - 0.000319)
c =
liquid specific
(accuracy
2 5 %J)
- 0.002349)
gravity
KJ/KC BTU/LB
“C “F
CAMPBELL
(T in ‘Cl (T in “F)
TOTAL
PROCESS ENGINEERING DESIGN _a . MANUAL SECTION
TEP/DP/EXP/SUR
FIG.
19
SPECIFlC
:
Date
: 2/8S
Page NO :
0
..
DATA
i
Revision
I
I
HEAT
OF HYDROCARBON
VAPOURS
AT I ATM
(NOTE
15-31
UNITS
ARE
BTU/LB/OF) I
PROCESS ENGINEERIF!G DATA
TEP/DP/EXP/SUF?
; .;I :CC
022
oc3 I’..
534
zc6 I
i
2,: :
DESIGN MANUAL
SECTION
:
32 ;
.”
.
c.3 !:
0.4 ! !
cs iIl;ln
0-e :o 1
I
;
6.0.
I
,o
I
! 10
I
. 5” 00.
g
I II;: illll
.
.
,
.
, -,,,
.A
Revision
:
Date
: 2/85
:t
0
j
2 :
;
! I I
I.4.i
j
1 I![
]
.,
:
Page No :
l-r 15-32
3 a
‘0 t ,:cc
i I I: ( ] I;
60
Illill
I II”
tXiii! 2.g’ id’ ’
2.0/r--
2.0
1.01 08 0.6
II, /l/I
IAll 1,111
I,,.,oO.l Illi]
0.00
ace 0.04
Lea ~reshre.
3 = f c
FIG.
19
HEAT MOLE/“F)
CAPACITY
CC
.,TION
(at armosphc .
FACTORS
(NOTE
UNITS
ARE
BTU/LB
-ssure) --
I’
l’
PROCESS ENGINEERING DESiGN MANUAL -fEPIDP.‘EXP/SUR
DATA
--
I
--
Revision :
SZCTION
Date
0
: 2/85
i PageNo :
15
-33
. FIG.
Approxlmat* of
20
rp.clllcg.ol hydrocarbon
copoclty rotloa gas..
TOTAL
PROCESS ENGINEERING DATA
TEP/DP/EXP/SUR
THERMAL
Revision
:
Dare
: 2/85
DESIGN MANUAL
SECTION
0
Page NO :
I5
CONDUCTIVITY
-34 Therm
I i
k
1 I-
tI
UNITS :
BTU/LB
1 STU/lb
“F
“F
=
1.1;SS Kcal/m.h.“C
t
I-
Use figs 22, 23 in this section t
.
Low pressure
thermal
conductivities
using : k=
/”
(Cf
accuracy
of pure gases and vapours *
+ y)
can be estimated
d
2 8 5%
k
- BTU/hr.ft”F
P CP-
’
,
lb/hr.ft BTU/lb
‘F
LIQUIDS .
Use fig 24 in this section or :
.
Liquid hydrocarbon k
mixtures
can be estimated
= -0.0677 sg
accuracy
2 12 96
using :
- 0.0003 (T - 32)
k
- BTU/hr.f t’F
% - specific T - ‘F
gravity
. SOLIDS See Perry of Kern for details of metals, earths and building
materials.
t r
r 3 060 L g 0.058 : 0055r I T 0 054fs 0052c
VAPOUR MIXTURE.5 .
;
.78 < > .95 32 < > 392
PROCESS ENGINEERING DESIGN MANUAL TEP/DP.‘EXP/SUR
Thermal
Date
Conductivity
of
1
I
;
Noturol
i
:
Gores
1
0
at
i
i
,----
Z ;
I 3060L..-
-L--
---
1
;
;
I
_
FIG.
22
,
----y -.
-
I
.-;
.-..-
Thermal
-
conducti%ty
ratio
’ I I
078
-2 0.026 5 p 0074 $
0021
5 OO?O E ; 0.018 f
FIG.
0.014
0010.
0
10
10
30
THERMAL CARBON
ro Molecular
50
60
70
80
90
100
Molt
CONDUCTlVlTlES LIQUIDS
-35
I
-<---y--.-L-c--“-L--w -..c-~,~~ -.” b.‘--‘--..V 2.I-r-ir*.L-.-r..
’I
,$ 0
r5
lobs)
--
:
,I
kPo
101.3250
: 2/8S
OF HYDROFIG.
24
23
for
goscs
PROCESS ENGINEERIf’!G
TEP/OP/EXP/SUR
DATA
I
.
DESIGN MANUAL
SXTION
TEPI
.i LATENT
UNITS
1 BTU/lb
BTU/LB
i
HEAT OF VAPOURISATION 1802 1730 1600 1500
= 0.5556 K&/Kg
Kcal/Kg
13oc
11oc
Use figures : 25, 26
100: 9oc BOC
Estimate using Troutons
rule : 70c
a
,OC
44
= 2l.Tb
cal/gmole
5oc
* c
For relief valve calculations Detailed
estimation
a01
Tb = boiling point “K
accuracy -+ 20 96
use 50 BTU/lb
if actual Lt.ht is not known.
methods in Perry : pp 238
I I I I
30(
'31 18[ 161
12(
1oc
9:
I
8(
I
6;
I‘ I I I I
7!
PROCESS ENGINEERING
DESIGN MANUAL :
Revision : 0
TEP/DP/EXP/SUR
*F
Date
.
l C LIOUID
1000
500
900 3--
I.
800-2 400
I I I
I( I‘
I
,-0+3,.
133
'",I Jlconol (I801 Ien.?*"* lutaoe (4) ,"lM. lutanc (430) 3”l~l l ICMOI (-I) IUl~l alcohol (-180) IUl~l l lcmol lutyl alcmol (.s*c) btyl l lcmol (.lOlT) :arooll dlollde :mbon dlsulrtdo :Jrom ktr*Chlwl~ :hlWlM :nlorotam >Ichlorwm~lmr (4-l >lrnIh~l amIn 3lP~fVI >kln*nvt )Iph*nyl NgtwlyI orId* N$rmnyl OXIda
307 263 152
n*m*nd urtnano Ycwv”l nlnrl *ethyl delhyt hlh,l 4*wl,l Y,h,kno MlOmJ.
124 267 265 265 23s 2;: 26a 143 nr
242 168 521
Sll 460 241 183 166 10 164 1SI 111 163
S
30
F
214 14s 267 2¶c 47 240
(-3) l IConOl l COhol amlm thlorld*
157 14)
CtllQlb IormolO cnlatd. omIti
214 216 %
O‘IO. (-3) ,-j (dull
n6 187 181 Y
PIOOMU
Proo,l
40
96
113 (CCI-FCCIF) 114 (CCMCCIF) (-n)
MlW~~ Dc1m* PwI1anc Ponunc
0
I
23s
Fwm Freon n.pt.nm
60
lc-I
111
Feeon 22 (CMCI)
I I1 I II
RANGE
.ceto*
IlfWW
I
I
‘C
,CIfIC .CIO
itnyi l ICohOl Ethyl l ICWW EthTl muIn* Ernyl cnlorlbe Ethylon* Ethyl-a Emyl.ww Etnyl .mr Fwon 11 (Ccl-F) From 12(CCI-F) From 21 (CHCI-F)
I.
: 2/85
alcohol
PlOpll l IcPnrl P,*IdlfU su,tu dlorlaa TSIWW Trlchlororth~)rrr “al”
(-ml
264
p-1
2% 344 lS8 121 271 176
l c
x
Y
105-200 140.240
5.6 7.0
11.9 10.2
ac-200 2ooJCO 10300 4070 70-200 IS175 17Odoo 150400 2OOd70 170-270 1-00 lb100 140-273 1oaoo la&200 176466 2oQjoo 125-200 lo-a2 22-160 lso400 50440 Jr0400 IO-1JO lb140 140.2S0 00-230 150-110 lb so lb-125 15-110 110-240 70-250 60-lS0 2O-220 SO960 4oGfSJ 4k2O0 lO&!70 SW40 10. SO IO-140 94ti40 100.200 lC.110 llbl20 lsa-Isa so-260 c- 25 25-12s 1650a (s-210 (WOO 16-262 l-70 ls-2s 2304so looGo lw-lW 1804OS lo-JSS
1.2 6.0 1-c 2.6 2.6 a.4 to 1.7 5.8 6.6 2.6 a.1 LS 1-c 1-s 2.7 '1.4 4.3 22 3.1 0.1 a.1
3.1 1.4 12.s 11.6 11.7 121 9.8 6.7 7.7 t-1 6-S 11.1 lJ.7 17.1 14.S lL7 11.2 6.6 16.2 16.2 12.1 1S.S
6.2
14.5
4.0 a1 4.7 3-s Cl 1.0 4.0 2.1 1.6 3.6 J.¶ a3 4.0 as a.5 a.4 a4 1.2 33 1.6 4.1 2.6 s.2 1.9 1.0 1.2 LA 1.0 3-J a.2 ca 21 a 32 7-3 20 IS 6.0 a0
¶.6 7.0 6.1 s.0 122 s.3 O-6 rt7 1t7 17.2 17.2 15.4 lL.1 11.7 12.7 13.5 11.1 6.1 1.1 4.7 6-S 11.1 11.2 11-J 13.7 6.2 12.3 11.6 12.: 12.7 11.0 a.I Cl 12.5 123 11.1 11-t 1.:
18 3
1s
0 - 30 20 19 18
- PO
ri - so
16 1s 14
- 60 - 70 - 80 - 90
Y " 10
-100
9 8 7 -150
6 S a 3
200
2.1
11
I
I I
I
I 7
I 8
I 9
1'llII 0 0
"iiI 1 2
3
4
S
6
I250 10
X
300 3so 400 aso SW 550 600
Exemplc
: Pour
I’oau
A 100-C 538
.
1, - t = 27S”
k-l/kg
I LATENT
-
-
700
-~4i20
I
10
- 20
-S
20
-
HEATS
OF
VAPORIZATION
OF VARIOUS
LIOUIDS
FIG.
25
PROCESS ENGINEERING DATA
TEP/DP/EXP/SUR
DESIGN MANUAL
SECTION
Revision
:
Date
: 2/13s
0
Page No :
15-38
1’ I I’
_(
Ii I
‘3 Y . 2 u Y
i= a
IL
0
IO -LLl
’ :;I
i ill!
I Illli
i!Ilii
;
LATENT *
--
PRESSURE
HEAT
HYDROCARBONS
- ATM
OF VAPOURISATION FIG.
OF 26
TEP
PROCESS ENGINEERING DES!GN MANUAL
DATA
I.10
SECTION
60/600,:
.U
20
UJ. ApI
30 GRAVITY
40 50
,TA INC.
1 --. 60
l7,ooO z 70
16.903
DATA
TEP/DP/EXP/SUR
SECTION
P
SURFACE
UNITS :
Dynes/cm
TENSIONS
1 dyne/cm
= IO-3 N/m
N/m 3 .
For surface tensions of paraffins
use fig. 28 w
.
To estimate
surface tensions for hydrocarbon
*
[5
l
~Gq~“,,.;,,,;
=
Parachor
18.07 + 2.946 MW for paraffins
=
278 + 2.35 (MW - 100) for paraffins
=
liquid density Ib/ft3
P’
=
vapour density Ib/ft3
T
=
P =
: 2 10 %
=
,ol
For oil-gas mixtkes
,use
*.
pccuracy P
liquids/gas
with MW < 100 with MW > 100
can also use
temperature
in “F
source: Beggs + Brill
pressure in psia
-
.):
PROCESS ENGINEERING DESIGN-MANUAL *,I ...
3 I, I.
TEP/D;‘/EXP/SUR
-1 I
I.
I
I
I ,1 ~ 1
DATA
Surfore
SECTION
tension
of paraffin
Revision :
Date
: 2/85
hydrocorbonr
FIGJO
23
20
IJ
IO
J
0
0
28
Page No :
L
‘5-41
PROCESS ENGINEERING Tajyyyg
-
l *
DATA
TEP/DP/EXP/SUR
JO
.cl
DESIGN MANUAL
Revision
:
0
Date
: 2/bS
.
SECTION
20
60000
40000
II I.
-a”
-ro
-30
-20
-IO
0
20
r*mpcrolu*r. ‘C
dJ
60
80
100
1210
Ia3
PROCESS ENGINEERING DESIGN MANUAL
Revision :
.- ^’
DATA
-rEP/DP/EXP/SUR
0
I
SZCTION
I Date
I
: 2/8S
Page
NO
‘5-43
I I I.
203
so0 &hbil;fy
m
:oGo ?ressurr.
of noturoi
gores
zooo 3sio in rottr
ecloo
6om
ond brine.
:o.ooo
FIG.
38
Sdubility
SOLUBILITY
of
methone
in
wotcr.
OF NATURAL
FIG.
31
GAS IN WATER
:
PROCESS ENGINEERING DESIGN MANUAL _ . TEP/DP/EXP/SUR
DATA
T
SZCTI@fJ
Date,
: 2/85
EL44 Z
FIG, SolubWty
of wafer
33 In hydrocarbons
0.09 0.06 0.07 0.06 0.05 0.04
0.03
0.02
0.01
0007 0006 3 005 OOW
I
.!..,..I~.
Or!glnaI
35
40
Temperature.
45
so
‘C
St t!y WS!!
’
from Or. John J. McKctta Unkcrrltv ot Texas 5s
60
65
I 70
I
‘fib
75
80
I
‘I EF
PROCESS ENGINEERING
: ,i
Revision :
DESIGN MANUAL
0 I
I DATA
1-t TEP/D?/EXP/SUR a’ 1 I
SE’?TION
Page No :
Date
: z/es
/ZLQ 1
-70
-40
-32
-20
- 10
0
. 10
TEMPERATURE
DROPS
FOR EXPANDING
C;AS
I
-
.
- _-. -.__ ._ cIll,co,
Moletutor
mot).
..
.
..
Boding poinl @ 101 3 LPo (obt). fter8mf.J
point.
lc .
.
,
61 oe
105.14
.
170.5
lb9
....
10.5
18
5985 350 1018
3173
. ~. . . , . . .
‘C..
..
.
...., ,.
CllllCOl contlonll Prrllurr. kP0 (Obl). . . . ~. . . . . . . . . . . . . . , I~mp*rolw*. ‘C.. . , . . . . . . . . . . . . . . . . . . . O.nllly
@ 2O’C.
LO/“’
Relof~~c drnbily.
I..
Specil~c haol topowy. Ihcrmol
hrot
,
.....,. ... ...,. @ 15.6.C
LJ/(LQ**C)
conducli*ily.
lolard
........ . ...,....
?O’C/?O’C; J/(~*tn~.*C/rn)
01 rcporirolmn.
0 ?O*C
rJ/ru
01 LPo (obt).
441
1.546
(30/10*C)
I.0919
9.511 0.210
@ 1O’C
0.156
, , 826 @ 101 .I LPO
6700973LPo
indea.
poml.
1O'C
t4J.
lC .
COC.
. .
moi1
.
~ I ~.
f1.*ring
polnl.
‘C..
Damity
@ 2O’C. denrity.
S~~IIG
18eot capacity,
Ihwmol
conduclirltr. hrol
lotrot
V~ctolily,
R*(rocci*r floth NOIf:
ol ropotitotion.
mP0.t
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point.
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WJlulwl)
-.. __-
109
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999 @ 30.C
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0.109
1.4851 I85
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1.889
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8 1O'C 01 LPo (obt)
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. . . . . . . . . . . . ..I..................
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0.249
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,
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I I? -I_----._ .____.___ ,._ --_. CIy~ol SUllOlW,.* M*llwwl -.--m---s _-._. _ _ . . _.
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93
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575 CJ 1fJo*c
1103 I? 101 3 &PO
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TEP/DP/EXP/SUR
0
Revision
:
Date
: 2/8S
page No :
‘5-47 i
LP VISCOSITY HIGH
-- _-
.--.-_._--_
0
PHYSICAL
WATER
-----.
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-
STEAM
OF
AH0 TEMPERATURE
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Loowoyx)
PROPERTIES
WC
l o
low
OF WATER
Ix)0
‘sx
Loo0
zsol
/ TmllB
PROCESS ENGINEERING DESiGN MANUAL
Revision
:
0
:
i
!
DATA SECTION
1 TEP/OP/EXP/SUR
Oate
I
: 2/8S
15
-48
.I
! I i
Prcuurr.
Viuosity
l f Air*
vlscmn R-. lb/q
i i i :; j j , 11/ ’ 1’ /I4:
-
lb ICC: P3w.: x lo-: Temp..
: -100.
ua 4&
iii Eon 900 1.aJo llm
I.4m l.mn 1.&x 2.m
4M 420 43. 43.5 44: 4.15 4.-o : 4 75 : 5;o 4.95 : ,
2500 .XUJ 3500
4.m
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0
*
605 662 i6Z
3.32. 6 I4 6.76
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6.49 966 10%
7.33 b.39 9.17
1456’11.94 16.09 12.W 17x1
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so
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4lO! 4.55 ,
OF
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3.10
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Ill : S6R ’ 5.E SO? 6 I9 S.iS . S 91 4 6.06 su 6.06 6.12 62.5 643’661 6.3S.642: 662 6.69 . 6.i1 6.66
’ :
s4;
; 3.70
ST2 3 ;: Sk SW x97
5J.4 5 i0 6.05 6.42 STb f.16 5.90 S61
6.99 ‘bb: 626
6.99 ’ 6.95 732 ;;A& 6.03
7.02 ;z’
10.16 Ii.05
942: IO.11
5.89 9.46.
5.36 0.Oi
639, 6.63
532 5.90
1x5
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91:
’
i
1010
‘Cornpled bv P E L,lrr For ,ahk III 51 un#u l nd 1 (0 IUOD bra. it Vauerm~n ka;rrawcL&,. phrlacal Proprnlo of .\w and \sr Componcnu.”
COK?OlfTION
3.43
531 53
4~6,3.OZ.S31:S61
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i
-
;loo’Isolaxr~?5o
426 4s; 443;
4 42 4s4 4.6b 4.8j 4.9:
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:
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-
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bon
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I
I
10 l301’K..
PHYSICAL
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aad
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l-be waqxdioa of dry air is -kably wasunt atI over the globe and throughour the a&x uopxpbuc The proportions by ~olwne of tie vanou5 compooeno UC gkn b&w (after h F. Fkne’~. 1939. 1952).
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