Useful Properties of <Fib ids
This
This up-t
up-too-da
date
te
er
ac
es
es
ROBE
ROBERT
RT KERN
KERN Hoff
Hoffma
mann
nn La Roch
Roch Inc.
Inc.
It is im orta
orta
to reco
recogn
gniz
izee-th
that
at
ipin
ipin
ofte
ofte acco
accoun
unts
ts
mini
minimu
mu
numb
number
er ofst
ofstep
eps.
s.
ro id ba ic esig
esig info
info mati
mation
on an es enti
ential
al data
data
equi
equipm
pmen
en in hydr
hydrau
auli
li syst
system
ems.
s.
Expl
Explai
ain,
n, as requ
requir
ired
ed th un amen
amenta
ta rela
relati
tion
on hips
hips
uler
uler
er oull
oull an Da cy to appl
applie
ie hydr
hydrau
auli
lics
cs
Furt
Furthe
herm
rmor
ore,
e, spec
specif
ific
ic refe
refere
renc
nces
es \Vil
\VilIb
Ib made
made to desi
design
gn
data
data if no show
show with
within
in thes
thesea
eart
rtic
icle
les.
s.Th
Thes
ese~
e~rt
rtic
icle
les,
s,
th acco
accomp
mpan
anyi
ying
ng data
data an l'e,
l'e,fe
fere
renc
nces
es will
engi
engine
neer
er ju no ente
enteri
ring
ng this
this fiel
fiel
el to thos
thos
np
th
this
this firs
firs inst
instal
allm
lmen
ent.
t. Th
this
this seri
series
es
nl
ewto
ewto ia
defi
defini
niti
tion
ons,
s, nome
nomenc
ncla
latu
ture
re
luid
luid
il
co si ered
ered
Dens
Densit
itie
ies:
s: Liqu
Liquid
id
expr
expres
esse
se in lh/f
lh/ft"
t" [5a]. Fo exam
exampl
ple,
e, th dens
densit
it of wate
wate
is P 6 0 w
62.37
62.37 Ib/ft
Ib/ft at 60°F
60°F
Pres
Pressu
sure
re ha no prac
practi
tica
ca effe
effect
ct on liqu
liquid
id dens
densit
ity.
y. HowHowever
ever incr
increa
easi
sing
ng temp
temper
erat
atur
ures
es will
will caus
caus liqu
liquid
id to expa
expand
nd
lo
.\
:te
io
in
th temp
temper
erat
atur
ur chan
change
ge in pipe
pipe syst
system
em This
This expa
expans
nsio
io
acto
acto is
P 6 P , where
te pera
peratu
ture
re
ence
ence th olum
olum lo rate
rate
tu
where
is volu
volume
me
flow
flowra
rate
te at 60°F
60°F
58
DECEMBER
1974/C
/CHE
HEMI
MICA
CA
23, 1974
ENGI
ENGINE
NEER
ERIN
ING>
G>
Pipi
Piping
ng-d
-des
esig
ig
te
calc
calcul
ulat
atio
ions
ns sh ul
io
lt
made
made at flow
flowin
in
ti
Specif
Specific
ic volume
volume
ft3jlb.
ty
ec
al
=:
ljp,
la
at
c, and
at
(1)
P601/P60W
S60
en
in
th
al lu
in
redu
reduce
ce pres
pressu
sure
re an redu
reduce
ce temp
temper
erat
atur
ure.
e.
Example
ar
ia an
ro Tabl
Tabl
we find
find that
that th crit
critic
ical
al pres
pressu
sure
re
iv
P/P60to
where
If
if
is th dens
densit
it
en itie
ities:
s: Vapo
Vapo
of liqu
liquid
id at flow
flowin
in temp
temper
erat
atur
ure.
e.
an
Ga
PV =: RTz, where
is abso
absolu
lute
te ress
ressur
ure,
e, lb/f
lb/ft'
t'';
';
spec
specif
ific
ic volu
volume,
me, ft lIb;
lIb;
univ
univer
ersa
sa ga cons
consta
tant
nt (ft)
(ft)(l
(lb)
b)j(
j(lb
lbXO
XOR)
R) an
=: I) Sinc
1,544jM, wher
ga (u uall
uall
Sinc
wher
th mole
molecu
cula
la weig
weight
ht
=: 144P', where P'
lute
lute pres
pres ure,
ure, psia
psia an
lI
la
be ewri
ewritt
tten
en as
Tz
density,
p,
1O.72Tz
rt
.e
is
(3)
1,544T/M
as:
---,
---,
l.
is
(4)
lb/ft"
AsEq. (4 show
show ga dens
densit
itie
ie depe
depend
nd on pres
pres ur an
temp
temper
erat
at re Henc
Hence,
e, fo purp
purpos
oses
es of calc
calcul
ulat
atio
io
pipe
pipe
in
te
es
ly
this
this
cula
cula
iz
Spec
Specif
ific
ic volu
volume
me is th reci
reci roca
roca of ensi
ensity
ty
ft /Ib.
/Ib.
high
high temp
temper
erat
atur
ures
es an pres
pressu
sure
re ga es do no
foll
follow
ow cl sely
sely th idea
idea as law,
law, an
:j:. 1. Th nume
numeri
ri
CHEMIC
CHEMICAL
AL
ENGINE
ENGINEERI
ERING/
NG/DEC
DECEMB
EMBER
ER
23, 1974
59
Pipi
Piping
ng-d
-des
esig
ig
te
calc
calcul
ulat
atio
ions
ns sh ul
io
lt
made
made at flow
flowin
in
ti
Specif
Specific
ic volume
volume
ft3jlb.
ty
ec
al
=:
ljp,
la
at
c, and
at
(1)
P601/P60W
S60
en
in
th
al lu
in
redu
reduce
ce pres
pressu
sure
re an redu
reduce
ce temp
temper
erat
atur
ure.
e.
Example
ar
ia an
ro Tabl
Tabl
we find
find that
that th crit
critic
ical
al pres
pressu
sure
re
iv
P/P60to
where
If
if
is th dens
densit
it
en itie
ities:
s: Vapo
Vapo
of liqu
liquid
id at flow
flowin
in temp
temper
erat
atur
ure.
e.
an
Ga
PV =: RTz, where
is abso
absolu
lute
te ress
ressur
ure,
e, lb/f
lb/ft'
t'';
';
spec
specif
ific
ic volu
volume,
me, ft lIb;
lIb;
univ
univer
ersa
sa ga cons
consta
tant
nt (ft)
(ft)(l
(lb)
b)j(
j(lb
lbXO
XOR)
R) an
=: I) Sinc
1,544jM, wher
ga (u uall
uall
Sinc
wher
th mole
molecu
cula
la weig
weight
ht
=: 144P', where P'
lute
lute pres
pres ure,
ure, psia
psia an
lI
la
be ewri
ewritt
tten
en as
Tz
density,
p,
1O.72Tz
rt
.e
is
(3)
1,544T/M
as:
---,
---,
l.
is
(4)
lb/ft"
AsEq. (4 show
show ga dens
densit
itie
ie depe
depend
nd on pres
pres ur an
temp
temper
erat
at re Henc
Hence,
e, fo purp
purpos
oses
es of calc
calcul
ulat
atio
io
pipe
pipe
in
te
es
ly
this
this
cula
cula
iz
Spec
Specif
ific
ic volu
volume
me is th reci
reci roca
roca of ensi
ensity
ty
ft /Ib.
/Ib.
high
high temp
temper
erat
atur
ures
es an pres
pressu
sure
re ga es do no
foll
follow
ow cl sely
sely th idea
idea as law,
law, an
:j:. 1. Th nume
numeri
ri
CHEMIC
CHEMICAL
AL
ENGINE
ENGINEERI
ERING/
NG/DEC
DECEMB
EMBER
ER
23, 1974
59
COMPRESSIBILITY
critical
critical temperature,
temperature,
ia
an 548°R
548°R resp
respec
ecti
tive
vely
ly We then
then calc
calcul
ulat
at redu
reduce
ce pres
pres
sure
450/1,073
T/Te
perature TR
760/548
.3
find
find that
that
.9 or thes
thes valu
values
es
rela
relate
te th
S60g'
P60y'
P60a'
un er th
am
co diti
diti ns
My
(5)
IIIIUlIIUIJWllllmIUllIlUIUIIIllUJIIIIIIIIIUIlIIIIUlilUlllnml!llJIIIUUlUllllllUIiIWIU!IUUIUIItIIIUHIlIIllIUIIlIlIllII1t1l!l
l Ulllnml!llJIIIUUlUllllllUIiIWIU!IUUIUIItIIIUHIlIIllIUIIlIlIllII1t1l!l!tllIIlflt
! tllIIlfltll1llllllllll
l l1llllllllll
S p ~ ~ ilil i H e a t
Molecular
a t 6 0 ° F . Pressure.
Psia
/c
I lili IlIl i
f(
so
Temperature.
Acetylene
Ai
Ammonia
17.03
1.31
Benzene
78.11
1.12
70.91
1.36
64.52
1.19
73
1.657
C a rb
rb o n d io
io x id
id e
C a rb
rb o n m o n o xi
xi d
Chlorine
th
y,
le
th flow
flowin
in temp
temper
erat
atur
ur
Ethane
a'
at
an pres
pressu
su e, th rela
relati
ti
is
where
is th dens
densit
it of th ga at flow
flowin
in temp
temper
erat
atur
ur
an pres
pressu
sure
re
Th de sity
sity of air,
air, P60a' is0.0 64 lb/f
lb/ft"
t" an th mole
moleccular
ular weig
weight
ht
is 28.9
28.97.
7. Dens
Densit
itie
ie an spec
specif
ific
ic grav
gravit
itie
ie
[2,4,5a).
Hydrogen
2.02
Methane
M e th
th y l a lc
lc o h o
M e t h y l c h lo
lo r id
id e
N a tu
tu r a g a s'
s' :
Nitrogen
1.40
28.02
Oxygen
49
22
73
27
Propane
Propylene
Mixt
Mixtur
ures
es
liqu
liquid
id-v
-vap
apor
or mixt
mixtur
ur occu
occupi
pies
es
93
E t h y l c h lo
lo r id
id e
Ethylene
(6)
Dens
Densit
itie
ies:
s: Liqui
Liquidd-Va
Vapo
po
E t hy
hy l a lc
lc o ho
ho l
W a te
te r v ap
ap o
of volu
volume
me th
=Approximate
1.33
18.02
vaue
Sourc
Source:
e: "Engi
"Engineerin
n eerin
ba
on av ag
composition,
Data
Data Book-1
Book-195
957,"
7," 7thed., Natura
Natura Gasol
Gasoline
ine Supply
Supply Men's
Men's
Assn.
volume
60
it
occupies,
give
give it dens
densit
ity:
y: P v
W/V
lllllllHIIlIllIUtllUlllllll1I1lIHlUHlI!1llllltllllllUllIItlUllllllltllllttlttt!tlllltltlUHlttltllll!IIl1/lHUllIIllllmlllltllUl!!ltlUllIlIHlIWlIIlIllltllllHi
D EC
EC E B E
2 3 1 97
97 4/
4/ CH
CH E I CA
CA L
E NG
NG IN
IN EE
EE RI
RI N
PHASE
an
vapo fo
ma eria unde goin
system-Fig.2
1111111111111
ible
Similarly, fo th liquid part
Wl+vjV
densit will be
th mixtur densit becomes:
Hv
WzlV Th
Since " 1 + 1 1
mixtur
lb/ft"
(Wjp )'
ca represen th weig
(7),
ture.
Example
water,
comp nent
(Wjpl)
PI
(7)
of fluid,
1.
crease densit significantl reduce th static head back
pres ur in
ertica pipe
2.
it
constant ei ht flowrate an
mall amou
vaporization th olum
flowgreatl increa es In
tu n, this increa es pipe resi tanc ignificantly uc
ei ht
Thermodynami
495 lb/h, an of steam, Wv
ar
el mixe an flowin co currentl in
11 psia
"F,
By ub tituting into Eq (4
find that stea
ensity
is:
0.23 Ib/ft3
18(110)
10.72(344
460)1
Properties
outine calculations fo piping an comp nent sizis
ly
it
useful to recogniz
he ph sica change take lace in
lo
if li id
it
il
le
iz
ly
pres ur eduction ca increa piping an componen
resistances.
[5a),
By ubstit ti
th
Pl
Men's
11I1I11I11ll1I1II
RING
is
/It.
th appr priate values into Eq (7),
it
500
(495/55.56)
(5/0.23)
16.3
ENGINEERING/DECEMBER
ta
lb/ft"
is
ll
1%)of vaporization greatly reduce liqui density Hence,
ig
aw
at
CHEMICAL
is
23, 1974
il graduall
np tu
es
in is ll
vaporize th liquid
in
hile it pressu
ts
an
61
1IIIIIIIIIIIIIIIIIIIIIIIIIIIIIIIImlllllllllllllllllllliUlIIIIIIIIIUlllllilmmlllllllllllllllllllllllllllli1IIIIIIIIIIIImmlllllllllUlil!II1mlllllllllWIIIIIIIIIJI
Typica Sections of Stea
1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1
Tables-Table II
Typica Liquid Velocities in Stee
Pipelines-Tabl
II
ds
Pressure
Absolute.
Pressure
'.
Temperature.
Hea of th
a te n H ea t o f
t.
Liquid.
Evaporation.
Gage.
Psia
Psig
of
Btu/lb
Btu/lb
110.0
95.3
334.79
305.8
883.1
111.0
96.3
335.46
306.5
882.5
112.0
97.3
336.12
07
882.0
124.0
109.3
343.74
315.2
875.8
125.0
110.3
344.35
315.8
875.3
126.0
111.3
344.95
316.4
874.8
127.0
112.3
345.55
317.1
874.3
l P
. I
2 or l
dL
FIlS
3 to 1
0 to 2
Velocity. FtlS
Velocity. FtlS
Water
Pum
to
s uc ti o
t0
2t
4t
B o i e r f ee d
S lo p e
4t
sewe
H y d r o ca r b o n l iq u i d s
Pressure
Absolute.
'.
Pressure
Saturated
Gage. P.
Temperature.
t, of
Psia
PSig
400.0
385.3
--
444.60
76
h. 1 .2 45 .
449.40
p s
Di
00
70
21
3.
to
D i sc h ar g e l ea d s (short)
3t
49
1 .3 07 .
1 .3 63 .
1 ,4 17 .
V is c o u o il s
P u m p s u ct io n ,
00
h.
1 ,2 42 .
1 ,3 05 .
1 ,3 62 .
1 ,4 16 .
h.
1 ,2 39 .
1 ,3 04 .
1 ,3 61 .
1 ,4 15 .
454.03
440.0
( N o r m a l v i sc o s it ie s )
T o t a l T e m p e ra t u re . of
M e d iu m v is c os it y
Ta an
2. to
ue oi
0.
44
0 .7 5
3t
Drains
1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1
1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1
IIIUm llllltlllUilUIlmllllllllllllllll llHIII1I1IU IIlIIIHillUilltlllllllli1U1U IIUnltllllUIIIIlIIIIIIIUlillIU tlllllllll llllflllll lllllHlllllllllll illtllll1l
Ty
t,
il au
tu
in
th th te perature an th volu
in
of apor
superheated.
At higher constant pressure th boilin temperatur
il
ig er an le heat il
required to aporiz
th li id
th critic
oi (see ig 2) th de itie
critical temperature, th substanc
ju ab ve it is co idered apor
Ve
S a tu ra t e
Vapo
S u pe rh ea te d V a po r o r G a s
H i g h P r e ss u r e
Nominal
Pipe Size
Velocity. FIlS
V e lo c i ty . F i l
Velocity. FIlS
In
or
as
ss
3t
is considered liquid
20
Btu/lb).
Thermodynami properties fo variou substances have
ee establishe an ar availa le ar of typi al ag
ci
gh
o 1
o 1
o 1
o 2
an
th
el
ze
an
ne
de
00
an
70
he
[1,5b
R eb o e r d ow n c om e ( l q u d )
Flashin
he
R e bo i e r r is e ( li qu i
Liqui
li ui
is fl
ib
O v e rh e a
in near it saturation poin (als
il
t)
C om pr es so r
s uc t o n
C o m p re s so r
d is c h ar ge .
nl
greate th pressure difference th greate th vaporiza
s t a m u rb in e
O bt ai n s on i
nt
62
th li ui
32
v/,
p o n t a t s i n ce r
o r c ri ti ca l
v,
ropertie
25
20
0.5v/,
R e li e v a lv e , d is c ha r ge .
vave
00
50to 35
as
Re
phas flowproblem Th quantity of vaporize liquid ca
a n d v ap or )
c o nd e ns e r
v el oc it y
Vet
from:
68yk(P'
/p),
Itls.
I I I I U l l l i l l f t l l H H l l l l t l l l l l l l l U U l U I I J l l l I I I I I I I I I H l I I I I I I I U H l I l t l J l I I I I I I I J I l 1 l 1 l l l r m t l l l 1 l l 1 I t I l l t u l 1 1 l l l l 1 l 1 l 1 l l 1 l l l 1 1 l 1 1 l l t 1 t l l l l l l t l l l l l l l ll l l l l U l I l I l l l I l I l I I l
D E E MB E
2 3 1 97 4/ CH E I CA L
E N I NE ER I
1111111
111111111111
111111111111
have
.aders.
VISCOSITY
FilS
Example
07
F.
045
0100
075
5.69 lb/h
0200
WI
:0250
satu ated
to
wa er
to
Specific
l.5v/
v/,
ea
IIIIIIUIIIIIIII1I
ERING
IN
63
..
and
I m l ! ! ! l l l l U l I l t l l l l l l l l l ! ! !1
!1 1 1 1 1 1 1 1 1 1 l 1 1 1 1 1 l 1 l l l l t l l l H l I l 1 l t l l l H l U l I I 1 I 1 I I 1 I I 1 1 I I 1 I I I I I U I I I I I H l l l l l l 1 t 1 l 1 l t 1 l lH l l l l t l l U l l U l 1 l l l l l l l H I I U l I l H I I I I U l I I I Il I I I I I 1 I 1
Maxi
Maximu
mu
Velo
Veloci
citi
ties
es To Prev
Preven
en Eros
Erosio
io
M a x i m u m V e l oc
oc i ty
ty .
at cons
constan
tan pres
pressu
sure
re
At cons
constan
tan pres
pressu
sure,
re,
where b.
ta
mp
an
:::::
b.h/
tu
FIlS
. L iq
iq u
c ar
ar bo
bo nn- s e e
PV
p ip
ip e
RT, where
c/c
P h e no
no lili c w a t e
C o nc
nc en
en trtr at
at e
s u f ur
ur i
C o o i ng
ng -t-t ow
ow e r
a ci
ci d
12
w a te
te r
S a l w a te
te r
C a lclc iu
iu m c h o riri d
Ca
od
b riri n
>5
ol me
A q ue
ue ou
ou s a m in
in e ( m on
on o - o r d ie
ie th
th a no
no la
la m in
in e
10
W e t p he
he no
no l
60
L iq
iq u
p la
la s
v ap
ap o
o r u bb
bb er
er - n e
p ip
ip e
10
1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1
al co an
em
quantity
expo
expone
nent
nt Data
Data fo
and
in hand
handbo
book
ok [2,3
[2,3,4
,4,5
,5cj
cj
Fl
tu e)
lo
ar avai
availa
labl
bl
The
in engi
engine
neer
er
io
Velocity-A
id
ipel
ipel
el it
io
le ee
velo
veloci
city
ty is calc
calcul
ulat
ated
ed at give
give cros
crosss-se
sect
ctio
io
flowrate:
ft/s wher
wher
ql.f4, ft/s
ft3/S, and
Fo liqu
liquid
id-f
-flow
low calcu
calcula
latio
tions
ns
0.408(
Fo vapo
vaporr-fl
flow
ow or gas-f
gas-flo
lo
an
li
ag
stea
steady
dy
(8)
£i2)
calcu
calculat
latio
ions
ns
0 . 0 5 0 9 W/(d P)
(9)
where is velo
velocit
city,
y, ft/s
ft/s
is volu
volume
me flow
flowra
rate
te gpm.
gpm.
is weig
weight
ht flow
flowra
rate
te lb/h
lb/h
is inte
intern
rnal
al diam
diamet
eter
er .o pipe
pipe
is ga dens
densit
it at flow
flowin
in temp
temper
erat
atur
ur an re
sure
sure lb/f
lb/ft.
t.
Th rela
relati
tion
onsh
ship
ip betw
betwee
ee volu
volume
me flow
flowra
rate
te (Q gpm)
an weig
weight
ht flow
flowra
rate
te (w
(Qp/7.48)60
8Q
0.125(W/p)
p/
P60w'
500QS.
500Q,
it Pi;ow
62.37
62.37 lb/ft."
lb/ft."
Th init
initia
ia pipe
pipe diam
diamet
eter
er ca be esti
estima
mate
te by choo
choosi
sing
ng
reas
reason
onab
able
le velo
veloci
city
ty fo
spec
specif
ific
ic type
type of pipe
pipeli
line
ne Thus
Thus
fo liqu
liquid
id line
lines:
s:
in
(10)
0 . 5 0 9 W/( up), in
(II)
0.408(Q/u).
Tabl
Tabl II give
give prac
practi
tica
ca velo
veloci
citi
ties
es fo 'liq
'liqui
ui line
lines,
s, an
Tabl
Tabl IV fo vapo
vapo line
lines.
s. alue
alue of and
ar tabul
tabulat
ated
ed
in pipe
pipe manu
manufa
fact
ctur
urer
er
cata
catalo
logs
gs [5f}
ll
ch
ca
ed th
mu
ed
Ta
li
e.
Viscosity-Viscosity
liqu
liquid
id or ga flow
flows.
s.
me
in
tance
ance of flui
fluids
ds With
With incr
increa
easi
sing
ng temp
temper
erat
atur
ures
es liqu
liquid
id vi
cosi
cosity
ty decr
decrea
ease
se an ga visc
viscos
osit
it incr
increa
ease
ses.
s.
Fo meas
measur
urin
in visc
viscos
osit
ity,
y, many
many Engl
Englis
is an metr
metric
ic unit
unit
el
ie
en
be used
used
conv
conven
enie
ient
nt conv
conver
er io cale
cale betw
betwee
ee th vari
vari
it es
FLOW
64
ai
ig
MB
3 , 1 97
97 4/
4/ C
MI
IN
IN
(12)
piS
where
and
is
isco
isco it
in cent
centis
isto
toke
ke
f1
/s.
is
f1
[5d].
,nol
,nolds
ds
re
umbe
umbe
Fric
Fricti
tion
on Fa to
re
rp
fl
is la
ic
(Fig.4c).
eyno
eynold
ld
numb
number
er
RELATIVE roug
roughn
hnes
es an fric
fricti
tion
on fact
factor
or char
chartt-Fi
Fig.
g.
Re
.t
s,
0)
1)
ld
re
he
st-
-isiits
vill
an-
FRICTION
fact
factor
or fo an
yp of comm
commer
erci
cial
al pipe
pipe unde
unde an cond
condit
itio
io
ING
H E I CA
CA L
E NG
NG I E E I N / D C E
ER
2 3,
3, 19
19 7
of flui
flui
flow
flow Fig.
Fig.
65
is dime
dimens
nsio
ionl
nles
es comb
combin
inat
atio
io of pipe
pipe diam
diamet
eter
er velo
veloci
city
ty
DUP/fLe'
dens
densit
it an visc
viscos
osit
ity.
y. Re
where fL
bsol
bsolut
ut visc
viscos
os
Ib /(ft-s)(ft2).
Prac
Practi
tica
ca formu
formula
la for calc
calcul
ulat
atin
in
Re are:
Re
50.6(Q/d)(p/Jl)
6.31
Nominal
Friction
Nominal
Friction
P ipip e S iziz e
Factor
P ipip e S iziz e
Factor,
In
where
we gh flow
flow b/h;
b/h;
is nter
nterna
na di me er of pipe
pipe n.
is dens
densit
ity,
y, lb/f
lb/f and
viscos
osit
ity,
y, cp
fL is visc
esis
esis nc
flui
flui
ot on depe
depend
nd on he type
type of flow
flow
Rela
Relati
tive
ve roug
roughn
hnes
es is €/
where
he bsol
bsolut
ut roug
roughhne (i.e
(i.e.,
., th dept
dept of he unev
unev nn ss of th in erna
erna pipe
pipe
wall
wall),
), an
and
shou
should
ld be easu
easure
re wi
he sa
di ensi
ension
on
unit
unit Valu
Valu fo rela
rela iv roug
roughn
hn ss
be ob aine
aine from
from
obta
obta ne
I l I 1 I B U I l U I I 1 1 1 I U l 1 1 t 1 1 1 l l l U I ! I I I tJtJ I I I 1 I I 1 l U l 1 1 1 1 l l 1 1 l lU I I I I H I I l I l l l l l l m l t l l l l l U I I I I I I 1 I 1 1 1 1 1 1 1 1 1 1 1 1 1 1 I I l I I l U l I l l lU 1 J l m I U H I I U I 1 I I I I I I I I I I I I I I H U I l l I
from
from Fig.
Fig. 6, fo vari
variou
ou flow
flow ondi
onditi
tion
ons.
s.
2,00
2,
000,
0,
th
fric
fricti
tion
on
Re
64/ Re
he
Re .;;;;
4,00
4,000,
0, th fric
fricti
tion
on fact
factor
or is unpr
unpred
edic
icta
tabl
ble.
e. Fric
Fricti
tion
on fact
factor
or
In
W,
0.0205
10
0.0136
0.0195
12
0.0132
0.0178
14
0.0125
16
0.0122
0.016
18
0.012
0.0152
20
0.0118
24
0.0116
11l1I1lJlIUIIlIHUllllllllllllllllllllll
l llllllllllllllllll
l llllllllllltlltllll
l ltlltlllllllJlll1HltlIIIIII
l llJlll1HltlIIIIIIIIIIIUUlllmlmm1
I IIIIUUlllmlmm1 1111111IU IlIUlUIIJIUI!I!llIlmlllllllJllIlIllil
J llIlIllillmmJIIIIIUIHlI
l mmJIIIIIUIHlI
manufacturers [51].
th re om enda
endati
tion
on
ards nstituteo
of he Amer
Amer an Na iona
iona
pipi
piping
ng an comp
compon
onen
ents
ts Prac
Practi
tica
ca form
formul
ulas
as will
will be give
give
fo liqu
liquid
id-l
-lin
in an vapo
vaporr-li
line
ne sizi
sizing
ng fo whic
whic th dens
densit
it
Acknowledgements
Re
ns
ig 6, th flowis
flowis in th rans
ransit
it on
urbu
urbu nt one.
one. er
th fr tion
tion fa or vari
varies
es wi he eyno
eyno ds nu ber.
ber. Th
nd th fr ctio
ctio fact
factor
or re ains
ains onst
onst nt with
with in re sing
sing
Reyn
Reynol
olds
ds numb
number
er
ec us gl ss nd pl st mate
materi
rial
al have
have smoo
smooth
th pipe
pipe
re at ve roug
roughn
hnes
es or pipe
pipe di
et r. Henc
Henc
tand
tand
xt
L. F.
here
here is on
References
[5e].
diam
diam te
in
il repl
repl ce he onst
onst nt re at ve-r
ve-rou
ough
gh
ns
borderline
Re
Fr tion
tion fa or in he to al
3. "A.P
"A.P.!
.!
C.
na
., "C emca
e er
er s
,"
turb
turbul
ulen
en
Example
B-S,
(I)
1=
th fr ct on fa to mu
be ob aine
aine
from
from
Rober
Rober Ker is
neer
neer in th
diag
diagra
rams
ms ar used
used in calc
calcul
ulat
atio
ions
ns wher
wher th pipe
pipe mate
materi
rial
al
eros
erosio
ion,
n, th fric
fricti
tion
on fact
factor
or shou
should
ld be incr
increa
ease
se by safe
safety
ty
fa or Fo team
team onde
ondens
ns te ooli
ooling
ng ater
ater al wate
water,
r,
size
size nd th
xpec
xpecte
tedl
dlif
if
of he ns al atio
ation.
n.
engi
engine
neer
erin
in
numberof
numberof articles
articles in thes fields
ha taug
taught
ht seve
severa
ra cour
course
se fo
desi
design
gn of proc
proces
es pipi
pipi g. plan
plan
u t g ra p i c i pi
pi n a n f lo
lo w
s, bo
in he U.
ci
Engl
Englan
an an th
and
th
laylays ys
ys ut
lo
U.S.
U.S. Mr Kern
Kern ha
an M.S. in mech
mechan
anic
ical
al
he
66
senior
senior designengi
designengi
corp
corpor
orat
at
depar
departm
tmen
en of Hoffm
Hoffman
annn- La Roche
Roche
Inc.. Nutl
Nutley
ey NJ 0711
07110.
0. He is spespecialis
cialis in hydra
hydrauli
ulicc-sys
system
tem design
design
si
engi
engine
neer
erin
in
Budapest.
E MB
MB E
3, 19 4/
E MI
MI C
IN
RI
:~ases in pipelinesundersteady-flowcon\ns.,
/'
ft
ROBERTKERN,Hoffman- La Roch Inc.':'
manufacturers' literature an
in
ec
thos acting agains th flow ar
in ha dbooks
at
in
em
ti
il
ap ly
tica formulas fo izin th components of such sy tems
when handling liquid an vapors
.l
'5:,F
Eule 's Deriva io
egative:
Pd
d l sin
in
an
ea
Pressure,
mass, dm,
En li me
em
ia ma
id is en
in
is dA.
and
aralle to it directio
of motion Fl
dp), and
(p
-_
p.
to show
dl,
b. Differential
Quantity
Enlarged
ei
dp dA
~"., sin IX
sin IX.
force,
hich is th flui 's re istanc acting agains th
io
0.)
Perpendicularl to th X-axis,
ct
th
al
each other, i.e. 2:
dm
(i.e.,
cos IX), er en ic
to
ir io
lo
Chern. Eng"
CHEMICA
(1)
dm__
in
pressure, (p
iv
Dec. 23 1974
p.
66.
ENGINEERING JANUARY 6, 1975
dz
FORCES acting on ifferentia
as in fl id-Fig
115
Point, .1
Ip
P1
2g
zo al
pe
DISTRIBUTION
length, dl, is dz
dl sin ex,
(2)
'iF
-:iF
adm;
W i g ; an acceleration is th velo
tional constant:
do dt Concity difference dv,
sequently, '2,F (W g)(dvldt). Sinc th weight.o flui
is it ol me ulti lied
de ity:
'iF
(3)
dA dl(plg)(dvldt
pd
where dlrd:
c . P ip in g T ur n
(5)
dz
relati ns ip
fl id lo
as develope
by
ga li es
er
iq id
re ur losses ar mall
pi elin
late in this arti le
2. Wher
en it cannot be co idered co tant
pressure differ ntia is izable betwee
is
Bernoulli'
energy dist ibutio Fig.
tw
hi
oi ts of th
la
Equation
constant yields Bernoulli'
equation
dz
Pl)
(z2 -Zl)
(2 in
ipelin
pressure differ
it constant diameter el city uall
VI
Th fi st fact chan es
th componen fo th velocity-hea
no becomes:
head differences, respectively Eq (6 is used fo investi-
difference
(7)
designer's standpoint Head loss
expens
re ure- ea
tatic-he
differ nce. Th
tatic-head if erence ca
ositiv
egative.
negative static-hea difference th pressure-hea differ
th h£
ractical esig
ork, Eq (7 ca ra el be ul ille
1.
greate than th re istanc
116
or calculatin
Fig. graphicall illustrate Bernoulli' energy distri
utio in
la te pi elin
it tw additi na factor
1.
an th
affect
gating energy distribution
uler
basi ways
line
PIPE elevatio
o wn wa r
to lo
Do no us up velocity head fo pipe resistance
2. Commercial pipe ar manufa tu ed in increments
of size (i.e., pipe diameter). Consequently th calculated
s am e
di
Eq (7 becomes:
o,
po
(8)
h an d
po
nd
pipeline
Resistance should be calculated fo al alternativ
he di
of
du
sure: Zz
ng
ns do
Zl'
of low,th st ti he adds pr ssur to th luid
of
flow
on
Zl
Zz
calculations.
.r>.
of
pe ne
g en e
sr,
tlPa
tlP
where /:"P
is'fhe
/:"P
pr
dr
ue
si nc
/:"P is th excess pr ssur drop
ug
q u m en t n d o m o n
pipe system ls introduces additional resist nces that
FLOW
10
/:,.P
resistances, th overall
tlP.
/:"P
tlP
dist ibutio
tlP
tlP
tlP
where
/:"P
and
ur dr
ue
si nc
pi
om on
is pressure drop du to resistance in equipment.
/:"P
/:"P
qu
C(2gh)
«v-».
(1
an be
of liquidthrough pipe or orifice-Fig.
liZ,
Flow coeffici nt or piping an pipe components ar
bt
om xp
da
or
ns
s,
or nt
usua constant is
When sizing pipes, th lo coef icient, K, is proportional to th rictio acto .j', an pipe
length,
diameter, D:
K==JL/D
"f
qu
he
om of he
nt
(11)
(Che n. En .,
ho
z.
or
of
pipe wall
liquid leve move down very slowly
nd it velo it
VI'
atmosphe ic at th liquid su fa
nd th bottom outlet
PI
and, consequently
O.For convenience, we will
ur
nd
bo
op
hL
thes actors into account, th Bernoull relation
reduce to
Taking
q. 6)
(9)
nc
ot
vi
ua
q.
lettin
hL
th
Formulas
convenient unit
by
gl sh
surement.
We il begi by converting Eq
10 to pressure drop
/:"P,
I:lP
ui
To ge pressure drop / : " P ,
ps or
(fL/D)(u /2g)(p/144)
I:lP
(12)
( h L P ) / 14 4
uc ng
pe
om
(13)
(10)
Ku /2g
CHEMICAL ENGINEERING/JANUAR
used by design rs manu actu er
ns
nt
on
ou
anc coefficient, K, an
Practical
.w
6,1975
117
velocity.asa volumetric flowrate Q, gpm, we substitute
(13). These
0.408(Q/d
D==d/12,arid
substitutions.now yield:
IfIlHtlllU1111111111111111111111111tJ1ll1111l11\\1Ulllm1l1111111111UIII!IllUjlllllluml!lIllllllllllUIIIIIltlt11 l11ll11l11l11l1l1l1Ulmll\\IIIIIIIIllJJl11l1Ullllll
Resistance
sist
90
in
of Elbows
quiv le
ip
ee
le
E lb ow s
N o m i na l
90
long
B en d
111,
pipe ength; t;
..J.L
is densit lb/ft";
Fl(
Vi~
co
10 ft
11
3.
3.
13
D.PlOO
O.0216fp(Q2/d
),
psi/IOO ft
(15)
q. (1 ca be ex ress
in term of sp ific gravit
by substituting
62.37
10.5
15
an
fa
(16)
21
24
10
Ex
at th flowin
2.
2Y
Sp
De
is friction factor
is
is volumetric flow
an volumetric flowrate must be expresse
temperature.
Through
Branch
4.
Sp'
(14)
Flow·
R= 10
In
ft
SUl
14
16
25
62.37 lb/ft", is
21
60 F.
nc
th
pe ific ravi
at
in
22
39
16
26
21
26
29
24
29
q. (1
12
Fo
or
5 ° e lb ow s a n b e d s e st im a
50
o f t ab ul a e d
80
returns, double th tabulate
values
16 ar th most onveni nt or
lc la
manufacturers' catalogs.
Example
32
60
an
in'') line
(J.D.
38
60
v al ue s
P60
(=321°F.
1IlIIIllHllIl\IIlI lI!1II11II IIIIl11\\\1 111l1111 1H!llUlI1 111lIUlltU IUlIIIlI1 l111[llUllllllllll!U\llllllIlllJlllJIII11Ill1l1111 11111n UlUIlII IIII\1U lllml\\l1l11l11 t1
I\lllltllllllt11111l111l1ll11lIlllill11lUUllllI1UI1l!IHI!\UIIUII!lI1111IllUIIII1U!l1mIII1\UlIlU!n!!tII11lIlUlII IUlllltlItI1!UI1IU\l11\l111l1llIlUUlllmlml\\\tllt\lIt1I1lIlII\UIlU\lI\U11U1II11I11Ut\IlIUH11111UU11I1IIHIlIIIII IUJIIIU1tJIIUUmUllIIUI11IllUllUIIllIl1III1I11l1ItlltllllllllllU\H11!J11l11l\111l11mlllllU1U1II1lIllU
is
Globe.
ce
in
ivalen
Pipe
Check
Straight·
~o
In
Straight·
60
2.75
70
3.
90
4.
Flow·
tI
Op
2.
2.25
tl
C o ck '
Ball
~o
1.75
2%
ft
T h re e· W a
Gate.
111,
le gt
F u ll y O p e n .
B ev e o r P lu g S e
N o m i na l
ip
ti
20
is
30
35
38
12
36
12
12
23
12
10
95
15
14
14
15
90
13
12
14
14
38
15
22
18
18
20
24
29
24
l os e
v al v s ,
va
30
38
40
17
20
17
18
it
45
50
21
20
64
25
78
lt
pipe area
80
UI1IU\\1III1I1U11111I\\1IUlIUtlJIIIIIII1l11l1111lH1IJIllUIlIIIUlUIIIIIIlIHIIIIIIlIIlIlUlIUlIIIIlIIl!IIllIIllI1I 1I1lUlUIUllIIlIIIIIlIIIIll1tl1U1llUllUllIIllIIlliUtlIIIIIlIllII111\!l\IUlIIII1ll11l\l\IIII1II1Il11Ullllllllllll llllllllllI1l11111l111\11UllllUUlIlIllUIIIIlItIllUl1l1lllltlllulmu\lIIumI1ll1ImUlllUllIJllIlIlIlIllIIlIlIlIlIll l
118
ti
Ii
17
12
(.
.,·-.:JANUARY6, 1975/CHEMICA
ENGINEERIN
r m I U I I U l l I I l l l l l l l I l l U l l J l l ! l l U U l I I I I I I l I t t I U U U I f J U I I l I l I U ] I U l U l l l l l l rm I l I l I t l U l l l U l I l l I I l I I l U l I l I l I l I U l l l l lJ l l l l l r m J l l l l t l l l l l l lm m l l l l l l l l l U l I U i
summarized as
Resistance
Specific gravit at 60'F S60
51/62.37
0.82
Specific gravit at 321°F: S 3 2 1
a,
1.'
Densit at 321°F:
62.37(0.72)
44. Ib/ft
Expansion factor
0.82/0.72
1.14
S60/S
Flowrate at 321°F:
900(1.14)
1,026 gpm
Qso/E
Viscosity:
1.'
Wenow calculat th Re nold numb
conditions:
of Ecce
(Resistanc
In
d,Ejd,
d,
Re
50.6(44.9/0.3)(1,026/6.065)
Re
1. 81X lO
ic
ft)
d,--dz
dz=t:::: d,
Sizes,
Yz
50.6(p/p.)(Q/d)
Co ce
in equivalent pipe length
Nominal
th flowin
Re
ic an
d,8
0.
0.
0.
0.
1.
1.
1.
0.
);,
y,
1Y
Re
of seri s, nd hence,
0.0154. (Flow
al in th ransitiona tu bu en on .) Substituting th
ppropriate values into q. 16 ie ds
t,p 100
1.35(0.0154)(0.72)(1.026)2/8,206
t,p100
1.92 psi!
1.
1);,
1.
1);,
3.
1.
.4
2.
2.
3.
in
(f4)
O.l25(W/p)
nt
t,p
nd
where I1P
drop psi/IO
q. 17
that (l)
(P
po nt
th m.
hi
onve sion
q. 17 be omes
MlOO
0.OO0336(j/p)(W2/d
15
9.
(18)
I1PlO
ft
P2)/2,
(17)
0.OO000336L(j/p)(W2/d
10 ft
12
ields:
is pressure
12
vi
where
is th dens ty
19
12
14
12
6.
th beginnin
nd
14
22
14
22
14
27
17
23
17
15
15
15
15
13
13
25
25
0.4P becaus energy losses du to accelera
tio'" ',a J.ddens ty va iation
an be neglecte up to this
10
ur
tion ar done by consid ring ha th line is divide into
14
10
course wi be diff rent in each segmen
0.IP
If
ve ag values of
al ul ted. ithe th do nstrea
or upst ea
ca .b used
12
18
densit
14
16
Example
12
4.02 in
1,05 in") ga
10,750 lb h; mo
lecula weight
16; temperature,
172°F; pres
sure,
12 psig an viscosity, fl
0.0145 cp
14
20
16
18
18
24
densit at lowing conditions
nd th
pipe an
ar
is
ea
ER
C he rn . E ng .
12
iction factor
Dec. 23
1974
it
he
qu
components
le
le
he
iv le
le
he
le
J l J l l U I U I I I U l I l U U U I I I l I U I I U / l l l l U U l H l I l l J I W m l m l l l H l l l l t / J I U J U l l l U l I l J I I I I I I J lI I J l I I U I l U l I I I I I 1 l I I I l U l U 1 1 I I 1 I I U I I I I I I I I U J I I I I I I U I I / l l m l l l l l l l l i m
119
AR
Ph,;:
;ealQ4,;;;U
, . P .4 M
)4
t_S#_
@ l4 , . . ,g;;S;
44P_.W?A
Q4iZ
Qt - 4J ! 4 .
;"
4t.A
U l l 1 1 1 l U l l U l l ! l l 1 1 1 1 l l l l tl l l l l l l l l 1 1 1 1 1 1 U U I I I I I 1 \ 1 1 1 ! 1 1 m U I I I I I I I l I l l l 1 1 1 1 1 1 U 1 t t l l 1 l 1 l 1 l l l tIt l t l \ l I l 1 1 ! m l \ n !
Resistance
lIlUnlmllll\1I1 !11~hlJ" lIl1ift'uu~tltlI11\11lfl1
ve,;tic~r
Horizo al an
Resistance
in equivale
pipe le gt
ff)
Resistance
y:_:
f= 0.23
Coefficient
1.
Nom ina
---,
P ip e S iz e .
--r=:
---.
0.
1.
:y
2.
4
1.
0.75
3,5
1.75
is comput d.
th Clxerallp essu
os "i lose to an
less than the. availabl:e pressure difference betwee tw
points in pipeline
select size is accept
fo th
give flow conditions
In pipeline calculations it is convenient to obtain pres
Multiplying tlP100 by
tlPlO
th equivalent length of pipe an fittings (L, ft) betwee
tw po nt ie ds th ov rall pressu loss
t::.P
t::.P lO (L/100),
(19)
psi
Th equivalent-pipe-length concep is th quickest an
most convenient method fo calculatin overal pressure
3
111,
5.
15
20
16
10
36
29
18
12
48
th tw ends of th piping component. Si es re assume
to be identical.
of
he
nc
ng
from Tables to IV
he
b l h av e
Example
pr
15
12
78
60
39
19
70
44
22
78
50
25
as sketched here
34
13
42
85
1 t l 1 1 l 1 l 1 U 1 1 1 t 1 1 1 U I ! U I \ I l U l l l l l m l l l tl U l 1 U I I I I U l l H l t n l U l l1 U l I l l l t lt l l l l 1 1 l l! l U I I I I lI l 1 ! ! 1 1 1 1 l I I 1 H l l l lt I l l l l l l l l l l l l l t l I U I I U I !\ \ ! ! ! u I 1 l IU I I H l I U l l l l I1 1 1 1 1
A l d im e n o n
temperatur
ng
re in abso ut units:
MP'
ha
1 0. 72 T
16(127
10.72(460
14.7)
172)1
0.334
Ib/ft3
Reynolds number
Re
6.31 W/ d,.,.
Re
(6.31)(10,750)/(4.026)(0.0145)
ft.
that th pressure drop fo th 100- oo length of th pipe
tlP 100
1.92 psi.
From able I,
dete mine th quiv lent pipe length
de
th
re
U s e l o ne -r ad iu s e lb o w s
Re
ou
we get:
sy
Actual length
78 ft
o ng -r ad iu s
e lb ow s
f lo w- th ro ug h
t ee s
60
158 ft
en
th friction factor
is
he
ft
20 ft
0.0166.
we obtain:
1.92(158/100)
04
on
th resistance coefficient, K,
K=fL/D,
nt
t::.P
t::.P lOO
0.000336(0.0166/0.334)[(10,750)2/1,058]
t::.P 100
1.82 psi/IO
ft
ng
O v er al l P re ss u r l os s
give se of flow onditions,
nd th overal pressure loss
itting an othe
ance of luid lo
3, 97
with orifices an
120
,, JA
omponent
ontributin to th resist
an be accurately added,
vi
flow nozzles,
RY 6,
9 75 /
me
E MI C
E N I NE E I N
CHEIII
aximum
iffe en ia
ss
an
si
.f
in
in
eas
rp es
ozzles
Flow
€)
e.
ea
tems must provid
equall important,
te
lo
pipe diameter of ufficien size and,
suitable configuratio fo th piping
amin
amet
in
at
to th sizing of orifices an flownozzles in piping systems.
th
lo
irede uate traight-ru
flow device
of piping before an afte th
ipin
ific
izin
Jan. 6,1975,
Ku
p. 117) to ex ress th
flow velocity as
(1)
Pr vision fo orific taps
separato chambers
it to
l
ll
trai htenin
vane
in
an
en
te
where
Vf!K
C, th orific flow coefficient.
(Chern Eng. Dec. 23 1974,
p. 64), we find th velocity-of-flow formulas
(2)
twee
pair of flange
thick) Minimu
la
ig ly
Usually, this orific is
orific bore is usuall
in If required
an
ar
ll
ific
ap
la
es
la
th
to
in
lo
2.
fluid, th pressure difference betwee
0.0509
stainles
/(ct;,p)
portiona to
where
passin throug
if
tw
19.67Cd~VJJ;_
(4)
157.66C~v1l;7
(5)
W,
give orific bore (do,
th
tl
id
th
th
es
L' ft.
(4)
th inle an outlet
meet your author se . cn em . E ng . . Dec 23,·1974 p:66.
selectin th orific bore an metering range, or fo sizing
ipe, th followin change ar nece sary
1.
os orific ma ometer
recordin an transmit
ting instruments) ar calibrated to in icat th ressur
F EB RU AR V 3 , 1 97 5/ CH E I CA L
E NG IN E R IN G
OR FICE mounts be ween pair of flanges-Fig.
ES UR
is ib io
lo
orific
un Fi
°F
in Thus
hrop
(h",/12)PGOto'
Valu
or:
ro
fo th
fi
orific
flow coefficient,
C, ar
st blishe
NR
(6)
Fo
liquid
Re
hI,
fi
(7)
(h",/12)(l/S)
re in
NR
(d
),
i.e.
do/d
or
hI
pipe.
In practica
and do
applications
Re
(5 yields
5.68fj2Cdy(Vh:;/VS)
(8)
359.43f12CdiVh::P
(9)
100,00 ar
capacity coefficients
For f3
0.7, f 3 2 C
is: (3
Eq
For (3
8) by S/SGO
fluid-flow
0.75, (32C
calculations.)
(32C,
0.339, and:
926di(Vh:;/VS)
(10)
121.87dh/h,:;p·
(11)
0.406, and:
2.31d~(Vh':;-/VS)
(12)
145.93diVh:P
(13)
h1
Fi t,
fi
b.
or b.
E NG I E E I N / FE B U A
3 ,1 97 5
(h /12)(62.37/144),
0.0361hw'
re
H E I CA L
valu
fo
NRc>
(d,,) to
do
00,000 th
re
73
..
acro th orific plate. As th high-velocit je from th
orific impinges upon th slower downstream fluid, some
of th jet' kineti energy converts back to pressure Thus
th
es
an th
Nomenclature
do
d,
0.7, th
of th orific pressure differential
ti
er
ak
lo
permanen loss is 52
Second, hw
ia
or measurin
at maximu
measurin
iq id
ra ge greate than th calculated deflection
flow At orma lo th de lectio houl
range. Practica instrument calibrations rang
ea
id
ti
ic
iq id
ad
stream of th orific ca overcome possible vaporization
Liquid-vapor mixtures cann be eliabl measured with
differential-pressure producin restrictions.
en
te
ft
Differential
S6
lo
in
Specific
e ig h
id
f 1 w ra te , l b/ h
f3
f32C
P,;o
Ca it
Viscosity, cp
it
iq
lo
it
lb/ft"
p(;O",
FU
larger flow capacities If th availabl
ce
in
di charge
an (9 reveal thre adjustment
ic
psi
hw
fi
ar
tiPo
p,
in
ie
hL
hw
to orific flow capacities
1. Increase Line
asin
li
entire straight-run of orific piping is th mo expensiv
tm
th is te
ce
to ac
er
ec
mi
manomete with
al
ca
th
me
ma
pressure difference
mp
high de lectio mi ht no
ti ty
th
i-
to
fice.
Th formulas fo estimating orific deflection from Eq
dia.,
ip iz is
ly
ip
diameters, an increa of tw pipe-sizes is also po sible.
ny increase in pipe diameter should be closel followed
2. Change Manomete Range-An
change in manomed
an ered es
al
Vh::
..,fh,;
ig
3. Change
0..0
<1
10
'>-
'>-
f-
f-
yp),
/(dif3
0.00278
standard 60°F
(S60/ S)2.]
in 1-
..
(j
'"
ru
ro
::
OJ
0..
0.2
da/d,
it
ca
ty
ie
{PC,
in
If
orific pressure differential an th percentage of permall
ea
me
at
Le us design an orific installati
fo it 3-i Schedule
3.068 in, d1
9.413) pump-discharge line Flow
50 lb/ft",
0.8, fL
1.3
0.7. fPC
0.339.
te
ey
er
th appropriat values into
NRC
Re
FE
sele
est,
rei,
6.P,
Ratio-Any
OJ
iil
On
(15)
.9
(j
Eq.
2.1:
cak
'/z
[I instrument deflection is calculated fo
liquid-flo calibration, hw
ti ed
Sin
exc
ges
50.6(Q/d,)(p/p,)
50.6(160/3.068)(50/1.3)
9 75 /
MI
101,500
lo
1113
in
inle
indi
adv
con
600/,
orif
defl
doe
sun
for
IN
IN
in
pensation.
to replac than th thin flat-plate orifice. To replac flow
ti
lo nozzle ca handle li uids it high vi co itie
an luid
it om ntrained olid
he ar uitabl
fo high-pressur an high-temperature services fo saturated steam, an fo high-velocit flui measurements
Thei applicatio migh be useful at existing installation
wher
ip izes ar to mall fo quare-edge
rifice
Fl w-no zl capacity an ipin ar size in th am
wa asthe components of orificesby usin Eq (8), (9), (14)
an (15) as applicable
than
Reynold
NOZZLE
0,00
alue
sually attained
ly
it ou diffic lty.
number
mounts betwee
Si ce th calculated
btaine from Fig. 3. Fo feasibilit in ma ufactu ing,
commercial size of flow nozzle ar limited. Th follow
flanges"':'Fig.
eynold number is considerably in
le
Vh;;;
7.9 inl/
0.176(1601 v'Q.8i/(0.339)(9.413)
hw
62.4 in.
hw
electe is 10 in
dol d.
Since
calculated: tiPo
th manomete
ca comput
rang
do as 0.7(3.068) or
0.0361(62.4)
relation to ti
0.70 52
ti
f:.P
0.52(2.25)
1.17 psi.
(100/62) 1.17
Betwee line-siz flanges,
of actual
ti
for:
1.88 psi
flow nozzle is held in plac
ll
advantag
of
it
flow nozzle istha it flow coefficien (and
ic
deflection th flow nozzle requires smalle
rati than
oe an rifice late onse uently th erma en
re
te
le
iz
IN
19
STRAIGHT-RUN
eeds fo
orific
pipi g-Fig.
75
CE R E FR E SH E R
Vena Contract
Taps
dia,
varies wit
ld
Radius Taps:
Corner Taps
dia,
r-2Y:.pipe cli".-l>I-""'----__;_-8
pipe di
---------1
pipe dia•.
Line Taps
in
averag
ratios an
capacity coefficients f 3 2 C
can
Orific Coefficients [1 ha publishe
pi
{J
{J2C
ipin
esig
or
perimenters. Th American Ga Assn (AGA)-American
an
ip
Co figu atio
on
ential-pressure flow-measuring element.
of th orifice. Th straight length increase with increasing
rati (i.e., ld ).
ni
before he orif ce is ffec ed by pipe onfiguration
nd
oc
ng
re
Th straight-lengt requirements afte th orific also
increase with increasing
ension us five time th pipe di eter fo al ratios,
standard arrange-
on
required straight length of piping fo orifices flow nozzle
an venturies.
ld rati of 0.7. Practica
GA-ASM
ch dule fo
orifice-piping arrangements usuall fall into on of thes
onfigurations. Th dimens on ho
in Fig.
re ls
suitable fo
ratios sm le ha 0.7.
Economy 01
ipin
.ayout
rge-diam te piping it heav
al th ckness or fo
expens ve al oy piping Occasional
quip en oc
tions, pipe connections, an predetermine distance ca
also intluenc orifice-piping dimensions Th minimu
straight-lengt requirements ar only possible if th do
calibrated piping
minimu
dimensiona
requirements
Ga flow
emoval
space
.!
u,
f-
U'-type control-valv
orific
assembly
bore
L iq ui d
fi
lo
in
to
fo vapors
ll
le gt
of inte co
ecti
ol
give th
malles
eflectio
Accessibilit
inst umen
in.
ecte
Separa~or Chamber
to
rifices.
ft
un
tUbi g. Fig.
i ni mi z
.•
an it in
te
ed
th
di ferential-pres ur cell This in tr ment is mounte in
th proximit of th orific flange (Fig 7) in an accessible location.
Differential-pre sure cell an manometers sh ul be
locate relative to orific flange so that interconnectin
~ t ~ ~ . 2 . . · . · t : : r !f-------l
':,
Meta pipe
(thin wall)
ca
Pipeline
Multiple-Tube
Straightenin
ed
ca
le
im
affect trouble-free instrument operation.
is
Vane
la
at
ea ab
clos to th orific an contro valve. Spac requiremen
is
ar
Tr mi te an
trollers should be accessible
Th
traight-length requirements enable th developmo in ma
.Cover
straightenin
ea
rack abou .5
two
th
ir
if
an
ar
id
(o in tw levels in yard piping th minimu horizontal
vibration.
Wher only metering flange an taps ar provided an
only occasional flow indication is needed access by port
able ladder is ufficient.
Locall mounte indicating an measurin flowmeters
ar mo frequently in pected If necessary, permanen
at
ac
id
is te
ar instrument fo measurin flow in rocess feed lines,
produc lines, an utilit lines.
it
as in
le
an
en
th
ts
present. Th same flow conditions ma also be develope
with straightenin vanes, whic requir
shorte straight
li
co
function an
et
id
le
tr
henc
ep ts
ll am
ir
measurements will be inaccurate
vane an only slightly correcte
if er
li ly ex
in th shor
at er
la in
ci
ib ti
ca
ta
th
tr
enin vane preceded by an elbo Manufacturer of thes
ic
ca
ec
en
ll ti
ct ce
at
an
me
il
iv
th
ASME schedule [1].
3, 1 9 7 5
tube
pito tube an rotatmeters,
References
I.
p re nk le , R . . , P ip in g A rr an g m en t f o A c e pt a l e F lo w M et e
Accuracy, Trails. ASME, 67 34 (1945)
l,
American Ga Assn., Arlington, Va., 1963
Chem Eng.
sufficient.
Locall mounte
indicating recordin
an
tran mit-
constant
wher
(",,Ie,,.
0.0509 W/(d p)
p.64:
0.0509 W(vp), in."
mp
al
it er ca
lca
an
at
es ar
ls
ai le
lo ly
mo ly mo te
it
i n Ibn/(ft-s).
(9)
(11)
f~
'I\l
.
.
,
,
,
.
e"
Ar>.,'
ipin
I!OI
layout st ea li e-fl
associated inst umen
co
an
co
itio s,
ec io s.
,~~
~~
ROBERT KERN Hoffmann-L
or meas ri
accurate
lo
fl
in roce
mete in
line
Roch
Inc.
us co ider
ig
or th job.
(Chern Eng.,
th
ti
venturi, it velocity increase an pressure decreases. Th
resultin differential pressure is proportional to th flow
at
nd is used fo lo mete in
in
72),
enturi
pito tubes, fl
tube an
temperat re an hi h-pres re services ompa ed
it
ot er entu mete s, it co is lo
ha
hort ve al
length nd hi
re ure- ec ve
characteri tics This
rota eter
en ur Flow Me er
ic
entu
is ve
small; an in
ll-d si ne
fl shed intermittently
in.
much ig er ca acit
izes rang
fr
to
yste s, venid
ha dl
vailable
ra
in ustria
applications
he lo
pressure
ra ge (10 to 1; some even
20 to 1) than orifices (4 to 1).
erly:
om th
ll
ta dpoi
pi in
esig
mu
esol
ve tu
is no as se itiv
to irre ularitie
in th velocity
th di ch rg
coef icient tays
th
flow data
2.
configuratio withou additional pipe length an fittings
Th alculati
roce ures ield th iameters fo th
inle pi an throat of th vent ri
anufacture s' cata
ratios.
of ventur [1].
sectio an throat metering accuracy is scarcely
by upstream flowdisturbances. Both ar availabl in
from
to
in.
Fo high-pressur an high-temperature services
previously describe meters ar also availabl as welded
Co me cial
en ur
eter
Th ventur meter' (Fig 1)consist of shor cylindrica
sectio having high-pressur connection an inle cone
id
·T
lo
an
be au
meetyour author se
Chern. Eng. Dec. 23, 1974, p. 66,
161
CE REFRESHE
Inle
.•
cone-...,
L o w- pr es su r
H i gh ·p re s su r
ta
ta
a. Ventur Nozzle
b. Short-Form Ventur
Low-pressure
c. Long-For
b. Welded
R ef . 1 ]
Ventur
DAL
f lo w tube ha
high pressu
Sizing proced re
fo
differential Fig.
enturi
eter (o an di ferc
re
.t
series (Chern Eng.,
umer ca va ue fo
he flow coefficients differ an
e,
th
orifices.
al
R ef . 1 ]
d. Flanqad-Insert Ventur
Liquid
at flowin temperature:
..;Ih,;
(1
S), gp
5.68/32Cdf.(
ic
0.176(Q·vs)i(dif3 C),
in
(2)
Vapors or gase at flowin conditions
ec
an
359.43f32Cdf.
V'h,;
ec
Th
an
differen ia
v'h;;Ji,
0 . 0 0 2 7 8 W/(dif3
yp), in
(4
pressure across ve turi
eters, I:.P
re
.P
(h /12)(62.37/144)
ps
0.0361h
zi
(5
co
en
venturi.
162
id
M AR C
3 , 1 97 5 C H M IC A
th,; most > 1 , .
EN
E ER iN G
Nomenclature
ri
i am e
Gravitationa constant 32.2 ft/s
om
lo
do
hw
(K,/v)
S60
f3
diameter of pipe
Capacity coefficient fo venturi
Flui densit at flowin onditions, Ib/f
iqui densit at 60°F Ib/f
it
62
b/
j32C
Pressure Distributio
P60
Alon Venturi Tube
Capacity coefficien for Annubar
Differential pressure across ventur meter, ps
Volume flowrate at flowin temperature, gp
Specific gravit of liquid at flowin temperatur
Sp cifi gravit of liquid at 60
Weight flowrate lb/h
P60w
0.7
0.6
o,
f3
Th
0.5
maximu
f3
0.4
?: 0.3
'u
ro
ro
cal-upflow or -downflow: or inclined position providin
0.2
as
horizontal.
0.1
Dall flo
ta
tube
0.3
0.6
Ratio,
0.7
le
ig
ee
dpld1
(3
Permanen Pressure Loss Throug
Ventur Meters
'" Short-form ventur tube
ventur nozzle
80 \---,...".,-+---120
te
with f3
ia eter is adequate
Straig te in
(3
(3
L o n q - t o r r n venturi,short-form
venturi,venturinozzle (320
Flanged·inlet,enturi
(32C
Dallflow tubs
(32C
0.12
0.2
0.67
0.148 0.2
40
4.
33
240
EE
straig
un equa
vane ca reduce th re uire
up trea
Chern. Eng
8) Configuratio of th do nstrea piping ha no effect
metering accuracy Reducers
elbo
ca be la ge
/MAR H3
valves locate
320
17.9
8.94 10.9
PRESSURE drop an sizin dat for venturis-Fig
EN
0.63
f3
f3
id
0364 0.44
"In, of wate
CHEM CA
it
0.51 0.63
Typica Manomete Ranges for Venturi Meters
..fhw
it
ly
eva
0.35 0.45 0.5710.69 0.75
ld
en
io
it
ratio,
ld
Ratio an Capacity Constants (3 C,
F9 Commercia Venturi Meters
Averag value, ( 3 , =
ta
pipe configuration. Upstream straight-run requirements
in
ti
Dall flow tube
90
Ratio,
ll
1975
io
ca
abov
th
grade.
lu
et
e,
co nections in addition to th pres ure- ensi
ta s.
ll
'63
'" High-pressure __
connection"
, li lt " ' "
""Flow irecti
".
Pip wal
Q)
+-'
Q)
J.
J.
-- On
or Tw Elbows
in Same Plan
::0
Q)
.9
io""""
·6
.~
,... """"
..,...
::l
J"
Static pressure
"./hole
'0
--
-1
rltL.----
\1Ur---
L~wpre.ssure--4il-
4~~-+--~+-~~~~
2~~-+--~~-r.~~T-~-+--~+--i
O~~~--~~~~--'_~~--~~-J
0.2
B.
0.3
Ref: [2
Re
UPSTREAM straight-run
op ning
ilot
nd valv
Pito Tube
b. Double·Venturi Pito Tube
21
fo ventur meters-Fig
should be
cessible
th pipe in
pito tube must be precisel lo te
an av ag velo
it
maxi um ve ocit poin an orie te in th di ec
wpa
ubes
if
me su emen
ue to thes cond tion
must provid
ir
difler ntia pr ssur
onventiona
pito tube Fig. 5)
Be ause of th sing e, sm ll im ac hole th pito tube
164
ga lines)
xc llen or me su in
high velo ities, av
hrgh·c pa it
flow having VCf)
ng
nd
easy
smal ventur is added. Th double-venturi
IiIfflmgeilien'
MARCH 3, 1il75/CHEMICAI.. E N G I N E E R I N G
I l i l l lU l U l U l I l i u m l l U l l I l I lU l W t m t l U l l I I l l I I J Il U J J I I U l l l l l l J U l I l l l l U u u u n U U l I l I l Il I l l l l1 I J I U I I I I I I I U l l i H I l I I IH l H l l l l l l I I I I II I I I l l I I I I U l I I I U I I I I I I Il I i I l I I I W I U l I I J l ! I I I J I U l l I l J l lU I I I I I I I 1 I 1 1 J U I I I J l l I U I I I I H I I I I IU I l l I l I l f I l I I l I lI J I I I I I I l I l J I I I U l l l U l l l f l l l l l l f l I l I l fH I I I I I I I I I J ! U U U U I I I I I I I I I I I I I I I! l 1 1 l 1 1 l l 1 1 l m l l u / u / U I I I
aigh
engt
Requiremen
fo An ubar Flow Elemen s- able
Upstream of Flow Elemen
Without Straightening
Vane In Pipeline
With ASME
Straightening
as Las Approach-Turn),
Pipe Dia.
Pipe
Configurations
in sa
Pipe Dia.
Di
Downstream
of Flow
Element,
Pipe Dia.
:3
plan
ow
wo planes
Redu,cer or increaser
Fully-open gate or ball valv
Partially-open valves
Glob valv
Note Contro valves should be locate
afte flow element.
1111111111111111111111111111111111111111111111111111111111111 1111111111111111111111111111111111111111111111111111111111111 1111111111111111111111111111111111111111111111111111111111111 1111111111111111111111111111111111111111111111111111111111111 1111111111111111111111111111111111111111111111111111111111111 1111111111111111"11111111111111111111111111111111111111111111 11111
ential et ee
th high-pre sure impact hole an
anom te
ef ec ions or
ro th
an factur rs
2C
ity coefficient
ub
av be
Fo ro
eliminat
impact hole (h h- re sure
four
ac
le
itot
Th
he
he fl
le
nt ca be nstalled deep be
ra
ith-
be an
itot-ven
for orific de
es
at s,
ca ac
th n'r a eragin
it
ide) facing th fl
do ns ream
ub
tu
direc-
(low-pre
w.
1,200° [3].
Form as fo izin
nn bars ar imilar
he rifice
form la
an fact re [3 pr ides
ca ac ty co
efficien as (K/,v)' wh~re Kg
ge etrica cons an
F; is velocity distri
tion fa tor, Fo rans tional an otal turbulen flow
F;
)'
0.82 Th capacity coefficient,
is analogous
C.
to th orific capacity constant
ipelines wher turbulen fl
xist
change
pipe size of th metering sectio is rarely necessary-s-an
PiP'7nlmF!tF!r
ing taps"
Static pressure ta
-,
'\
<,
Flow
.U
Throat
insert
Recrossed\
pressure nozzle
Do~nstream
ANNUBA
tube
mete is an averagin
CHEMICAL ENGINEERING/MARC
pito tube..,...Fig.
3, 1975
MP
ub
handle flow in either direct on-F g.
165
then only fo extremel
lo
or extremel
hi
fl wrates
selected Permanen
pressure loss is negligible
at
Th foll wi
able list om representative va ue fo
variou pipe sizes:
No minal,
In
Lo s s ,
(Kl,')
0.82
h",
.6 to 0.62
0.66 to
0_
to 0.75
to 0.78
to lY
1% to
to
to
to
to
<%
Instrument deflection at flowin conditions fo liquids:
Fo instrume
ca ibra io
at
stan ar
Noting position of float-head edge
(6)
in
h w = - [ 0 . 1 7 6 Q v 's / (K ' ! " v) d i) 2 ,
referred to capacity scal on glas
tube give flowrate readin
liquid-flow
S)
Instrument deflection at flowin conditions fo vapors
an gases:
(0.002 78 W/(KuFv)di
hw
ifferent al pres ur
t::.P
Straight-lengt
ob aine
60
P ]2 ,
...... ..
Metering float
(7)
from
I nl e f l a t s t
0 _ 0 3 6 1 h w ; ps
(8)
requirements fo 'pipin design as rec-
-Inlet
connection
Ref: [5
Th flow-sensing tu (F~g.7) co si ts of shor ho sng ec ion, an
symmetrica an tapere hroa sect on
avin
flow re tric io in he ce ter. Th throat sect on
er
am
ra
re
en
ti
tays co stant. In co tras
constant-restric io
an th pressure difference across th restrictio
prop rt onal to flow
Th ro ameter cons st of apered eterin
e.
es
e-
become
ub wi
ca
C(2gh)1I2. Exac formulas fo sizing this impact tube
re
Appl cati ns fo th impact fl
tu
ra ge from wi
ce
Straight-lengt requirements fo this device are; pipe
diameter up trea
0diameter
pstrea afte
throt-
Rotameters
Inro ameter
he area restrict on varies
prop rt on
to flowrate an th pressure difference across th restric16
re
libriu
when th pressure difference across th float, plus
an
In ai an wa er er ice, th viscosit effect of he 1u
on th rota eter re ai
ractical cons an Th ma es
poss bl he us of standard capacity able fo such flow
treams Standard sizing char s, tables
correc io facor fo an fluid, ta le
correction fact rs fo pres ur
an temperature, selectio guides fo type of rotameters
etc. ar availabl in manufacturers' literature [5]. Hence,
rota eter ca cu ations ar eldo ma
pr ce en ineers.
cr
Rota eter
er
ar
especially suitable fo vi cous iq id
wr
it
t}
lt
ti
P ip o
PIPING
arrangements fo installing
rotamete having alternativ
-[g~
ti
C o nf ig ur at io n
taps ar simple an economical-Fig
co
em
a pe ,
rr er
a br a
ew
ca ibrate
S uc h
an ac
to show (a fl id elocit
an
at
(b percen ag
con-
at
fe
er
racy Straight length of piping is no required Dependin
ip co figuration an rotame er design al erna iv
.t
provid simple an economical piping..arrangements
ro
er
ck
In cl an
rm
ro ameters,
by as gl be alve no necessar Locate
th flow-regulatin glob valv to th rotamete (a before
e te r
rv
houl be access bl an
th operatin aisle.
ex
et
%of
rotameter.
Rota eter calibrat on
av ifferentia ranges
th rotamete
scal visi le from
as
fl
fl
es
th
itti
ar usua ly nonadjus able an
0-50 0-10 0-150, -200 an
th flow signal
contro valves
References
1. Engineerin
ROTAMETER-ORIFICE
168
measures larg flowrates-Fig.
10
Informatio on Ventur Mete Tubes, BI Div. Ne York
A i B ra k C o. , P ro v d en ce , R I
2. Instructions fo Pitot-Ventur Flow Element, Taylor Instrument Cos.
Rochester, NY
3. "Technical Manual-Annubar,"ETliot1nstrumen
Div. Dietric Stand80302.
r.
l o T ub e D i . , B et hl eh em , P A 1 8 0 1 6 .
5 . " Va ri a l e A te a l o
e te r a nd bo o , " V ol . I -I II , F is c e r
Porter
Co., Warminster PA 189.74.
ControlValves
rmulas
nd
stalla io
rocedure
fo se ec in
ROBERT KERN Hoffmann
an usin
La Roch
ontr
valves or luids.
Inc.
tr
proces operatio
handling flui streams. Hence, we must
il
it
en
is
to
meet proces conditions an to ensure proper installation
th
ti
lo
lu valves enerally contro valves it rotating axes
ar suitable fora wide rang of flow-control applications
Ch ra teri tics
ls
tr
On majo grou of contro
co
ported Flow-control characteristic
al es esembles th
lobe
thei flow characteristic
Quic
in
lv
Valv Pl gs
ir
pening
depend on th shap
are:
single disk (for high tempera-
at
linear flow characteri tics an shor te movement
inea Flow-A plug ha linear flow characteristic
th lift
Equa
ercentage-
lt
ur acro an orific
othe flow-sen in element.
Th single-porte contro valv (Fig 1)find us wher
io to lo
capacity valv than th single seated ne of th same ize.
th
seated valv cannot shut of tightly. Th valv accessories,
an
conditions
To meet your author se Chem. eng., Dec. 23 1974 p. 66.
CHEMICAL ENGINEERING/APRIL 14,197
twee
thos descri ed
pl
as equal- ercentag
io
t-
an facturer
provid
diagrams
'A lu having linear-flo characte istics is commonly
specifie fo liquid-level control. Th equal-pe ce ta
ll
85
Single-Sea
contoure
Double-Sea (Equal-percentage
ported plug fail open)'
(Equal-percentage
plug fail closed
va
fl
available; or wher
ressur drop acro
c-
(als
called
sp
-F
th contro valv
te is ic
ce ta
control.
Actuator
Alternative
Actuator an Plug
perators
Butterfly
Valve
te is cs
al
positioner
valves av th actuator side mounte
ecause
es
ax e.
ct
in
th in
ac
valv axle
Th valv housin .and th operator's yoke ar
ll
th actu
ti
Bal Valve
separate
at
Camfle
Valv
available.
Safet
Requirement
ROTARY actuator
moves flap plug
valv ca be in cl sedo
86
or
open position Thes alternativ
APRI 14 1975/CHEMICA
is
ENGINEERIN
Lubricator fo
valve-stem
packin bo
Finned Bonnet
(For temperatures higher than 40
Bellows Bonnet
(Sea betwee valv an
packin bo in toxi service)
Extensio Bonne
(Fo cryogeni temperatures
F)
Sid Mounted
Cas Mounted
Pneumati Positioner
(Or transmitted.
ACCESSORIE
ex en
(F
im
to
(Restricts stem movement
usefulness of contro valves by prov ding fo extrem
po it on ar acco plis ed by reversin
at
an
Handwheels
ma al pe atio at
startu or ai failure)
unusua conditions-F g.
th seat ring an
orderly. shutdown procedures
On concer of he esigne is to se ec alve that wi
fail-saf in th even of nstrumen -a
fail re In princi
le
contro valv fail af if te perature an pres ur
valv become inactive
Fo example, fuel-oil co trol valves
heater urners
fa
(i most cases) shou fa open to av id verheating he
ee co ro
cl ed
ea
boi er
fa ls cl sed. Refl x-drum va or outlet an reflux pu
ch
at
compressor bypass lines, an reciprocating-machin
by
pa li es fa open
an usuall th feed-control valv fail closed Generally,
designer of flow system should consul process, instru
CHEMICAL ENGINEERING/APRIL 14,1975
Capacity Coefficients of Valves
Valv flow coef icie t, C"
dime si ns of th alve an th smoo hnes
es
Manufacturer
give th followin
c,
Q(
of urfaces.
ai
definition
VSivlJ»
6P::::::
Capaci
in exes fo th
ut erfl
va ve ar also give
CE REFRESHE •••
Nomenclature
c,
fT
C"
position
,"
D/d
Expansio
factor
M ol ec ul a
e ig h
Absolute
pressure
"so/p
ia
t:..P
r,
i f e re n i a
psia
p re s u re ,
ps
psia
reducers
p/
Sao
v,
Absolute temperature,
S o i c v el oc it y f t/ s
iscosity
LO
hara teri ti
of orte
or cont ur
cp
60°F lb/ft"
60°F 62.3 Ib/ft
P6
Ps
lu -Fig
PSOw
60°F
Subscripts
Upstream condition
Control-valv
coefficients for single and double-seate
Do nstrea
conditio
.
Calculate Flo Coefficient, Cve-When sizing contro
valves
flowcoefficient is calculated with normal design
io
te in gp
om
c;
Q(
VS;y"M)
downstream pressure,
av ta io
an be susp ted.
exceeds C v e .
flo
betwee
coefficient, or:
Cv/C
I'
he
brasiv flui is pres nt
Critical Flo Factor C, he pressu
vaporizati
ca be onsi er
ro
conditio
di mete of th do nstrea
he riteri
where:
gr di nt
ro
onside
ubcritical
th va or pressu of th
iqui
il no ge ighe ha th lo st pr ssur poin
ac os th ontrol va ve
po pres ur is he pr ssur
temperature. Tables of thermodynami properties of liquids give corr spondi
satu ted-liqu
ressur
an
temperatures.)
or subc it ca an
the
he va ve or this
ip
il usua ly
it ca
lo
in iquids
t:..P
C/(t:..P.)
(I)
s»
q( t:..P.)
(2)
s»
(3)
VP1/Pc)P.
and P, is th
itic
ressur psia
I Fo simplicity t.P
prov de
O.5P
he sizi
ormu fo
itic flow is
th
"c
article.
trifug
88
and
0.5 to 0.8
C v c / C ratios bu th plug willl:>~closer to th full open
or ul
lose po itio
nder hese onditions, we lo
he mportant ad an ag
limit
operabilit of th process.
or
upstream an downstream pressures,
pump Critic
lo
occu ac os
pressure-
A P R I L 14, 1975/CHEMICAL ENGINEERING
IIII11HunlmUlIllIIlI!l1!UllllllUlmnUUlIIUlllllmumnllUlIIlIIUlIUlIlIlIIlIIlIUlIlIlIlIlIUllIlIlIIlJII11111111111111111111111111111111111111111 11111111111
lo
lo
iz
Single-Seat"
efficien
il
as
ic
reache th soni velocity
C"
Double-Seat"
v.
.0/.
12
9.
1%
nois an
it
ft/~.
68Vk(~'/p),
(5)
vibration.
are respectively:
1%
/:'P
11
75
ti
0.5C,zPl
(6)
O.sqP
(7)
av id
C, value.
45
Th critical flow factor
1,160
1,620
2,000
16
Thes values have been obtained fo Masoneilan 10.000-serie (eithe
equal-percentage or V-port plug valves having full-capacit trim bu also appl
to simila valves of othe manufacturer [2].
1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1
is
dimensionles
number
C,
betwee
th control-valv
coefficien unde 'critica con-
facturers literature.
V a l B et w e
P ip e R ed uc e s -F lo w
it
correctio factor, R. In critical flow th correction factor
is Crr, whic replaces
lc
io
rr
size. r1 rr and
av values smalle than
Numerical
es
th
in
li te in
Letus
ariz
la
in
contro valves fo liquid an ga services unde di ferent
flow conditions [1].
Liquid Servic
S ub c i t c a
F lo w - Fo r
coefficien is:
(8)
if
position,
it
replaces
/:'P(min)
ar
P: PI
ve
(Q/C )2S,
psi
(9)
",
plug position betwee
expression is
I::.P
where
CvclCv
0. to 0.8,.a convenient
Cvc/C
(CvclCv)C
ta
S,psi
ct
(10)
at
).
la
ci
am
is
flow is
(II)
Cr ca
CHEM CA
ENGINEER NG/APR
14 1975
F lo w -I f
89
U l l I I lJ l l I I l ! ! l m ! l! I r 1 l 1 l1 1 U l l l n l l m l l l l f l l / l lU l m : U l I l I Il l I lI l I I l !l l I lI l n l lI l I l lI l I l U I I I I I I I J I I I I I 1 I I 1 1 I I 1 I ! I I I I I I I I I I I I I I I I I I I I I I I I I I U I I I I I I I I I I I I I I U J I U U I I I I I I I I I I I I I I I I I I I I I I I I U I I I I I I I I I I I I I I I I I I I I I I I I I 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 11 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 , , 1 1
l-
r
.
.
lv
lo
fi
li
le
Double-Seat*
ingle-Seat*
Condition
C ri ti ca l
V-Port
f lo w
1
_
C ri ti ca l
c;
f lo w
nt
be
r
-
(d
S ub cr it i a l
0.98
C{
f lo w
V-Port
0.98
or 0.85*
0.94
0.86
0.86
0.94
0.96
0.94
1.5
=:::
Equal-Percentage
Old
pipe reducers
._._-_.Thes values have been obtained fo Masoneilan 10,OOO-serie plug valves having tull-capactt
a ct o f o f lo w t o o pe n
' Fa ct o
trim bu also appl to simila valves of othe manufacturer
[2].
f o f lo w t o c lo se .
1 1 1 1 I 1 1 I I1 I I 1 I I1 I 1 I 1 I 1 I I1 I I 1 I 1 I I 1 I1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 I 1 ! 1 I 1 I1 I 1 I I1 I I 1 I I1 I I 1 I1 I I 1 I 1 I 1 I1 I 1 1 I I 1 I 1 I I1 I I 1 I1 I 1 I 1 I1 I I 1 I 1 I 1 I 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 1 ' " 1 1 1 1 1 1
size th simpli ie
becomes:
calculated control-valv
c.;
i\
(QIC,)(
coefficien
.re tl
(i.e.,
condition:
P,,)
provided P , , : 2 0.51'1'.
Th calculated control-valv
flow il be
::':;
where ::"P
or critical flow
coefficien fo subcritica
11.65y3P(P
provided th.a t::,p
he
,p
O. C/p
1O.13C,P1
If th valv is locate
betwee
(IIR2).
lv
el ithi
to th
or pi
wo
ize.
ls
Computation
n.sc/p!.
LI
b/
(14)
educers, multiply
Replace
(14).
cien ratio CveIC.,
Let
1 13 ,0 0
V;;;
pi
llustrate
(13)
P2)Pl
c, with
fT
in
iv
0. to 0.8. Th operatin
it
lv
in sizing valves fo critical flow ma
hase Flow
it
c;
44.8
y'Xl>(=(.]=+=(=.z==)-
where PI and
th
'phase densities respectively
tu
90
(16)
O.SC/P
(For calculatin
t::,p
th de sities in two-phase. flow ee Pa
of this series
Chem Eng.
ec 23 1974, pp 60-61.
Exampl
----.~--==
ve
63.3 ~l'fJ]
I!C
ic
pc
io
1'1)'
(15)
),
te
14
75
CE REFRESHER•.
I U l m l l J l U l U l U l U l J \ l l l I I l I l I U ! I I l l I l l I Im l l l l l l l l l l l l m m m l l l l l l l l l l l l l l l l l l l l m l l l l l l l l l l U l i l i l U 1 l l 1 I 1 1 1 1 1 1 1 l l l l l l l l l l l l lU l l U I I I I I l I I I I ! l l i U l U I I I I I I I I U I I I I I I I I I I I U l l l l l U I I l I I I I I I U I I I I I I I I I I I I I I I I I I I I II I I I I I I I I J I I I I I 1 1 I 1 U I I I l I U l I I I I ' I I I I I 1 1 I 1 I 1 I 1 I 1 I f I l I l l I I l l II l l I l U I I I I I I I I I U l I I I I I I I I I I I I J I I I I I I I I I I J I I I I lI W l I l I l I l I l I l ! U U l U l l U l l l I l l I
li
Ii
'"
:i:
..
<l>
No 1046
Bronze Glob
Valves (Threaded)
Stee Glob Valves (Flanged
Flow Coefficient,
Flow Coefficient,
Flow Coefficient,
Fo Valves
No 546P-150 Ps
For Valves
No 556-20 Ps
No 576-30 Ps
0P
Size,
In
Fo Valv
No 1040-150 Ps
Flow Coefficient,
Fo Valve
No 1042-300 Ps
No 1046-600 Ps
46
55
200
235
2~
29.5
24.
1~
400
41
Note Flow coefficients have been obtained fo valves manufactured by Jenkin
Bros.• bu also appl to simila valves of othe manufacturers.
11111111111111111111111111111111111111111111111111111111111111111111111111111111 1111111111111111111111111111111111111lIIIIIIIIIIIIIIIIIIIIIIIIIIIIIIIIIIIIIIIIII IIIIIlimllllllllllllllllllllllllllllllllllllllllllllllllllllllllllili11111111111 11111111111111111111111111111111111111111111111111111111111111111111111111111111 111111111111111111111111111111111111111111111111
-f
estimates, will have mino effect on valv capacity Thes
ar smal values=-square-roo function of th calculated
w c
Wh
ritica lo occurs in th liquid th piping fter
nt ol
ve
ou be
ul
sized. Vapori atio
in re se pipe resistance consider
bl To stay ithi easonabl velo itie when vapo iza-
he up
pi
me
of
he
ve
hi
or la ge pr ssur
op
os
vertically up}Vard.A control valve will operate in angular
hori onta or vertically downward position Neithe pipin designer no operator
ccep th se positions. arge
angl -control valves re an exception;
hori onta posi
ypaS in
on
bypass is usuall
on
lv
provided fo contro valves sm ller
ng
ve
s,
single ontrol valv withou bloc valves an bypass
is usuall sufficient in clean-flui service; or wher paralle equipmen
ontainin
ontrol valves is installe
it
oi
or soli particle
reducing stea
on
on
92
contro
ou
ut
qu
valves with th flow coefficients fo double-seate
va ve
ob va ve or
nu
ll oper te th ottlin valves in th same ay
contro
valves provid
that flow coeffici nt ar av ilable
o w v ap o
of qu
st
no
he ng ne
At high pr ssures high temperatures
nt
he
nt ol va
ul
.fo om
on
uf
be
ve
se of
va ious seat ana-plug designs, valv coef icient ar no
s am e
mp
be va ve
de by
nt
manufacturers.
an be oc asionall
expe ted,
tempo-
service.
ng
va ve
n,
st
ow
ow
nt
operators.
Most piping specifications call fo contro valv
APRI 14 1975/CHEMICA
to be
ENGINEERIN
~ ~ > < ]T c k G )
_d"l
'"
~r
. . , " '; = . " . " . . . _ "- " . , ., . , " ", " "
. . ". -,....,,7"1
:;
'0~?
MANIFOLD
an bypasses fo installing contro valves into th proces piping requir
tion syst m.
proper clearances an drains-Fig
ensing points or lo
pressu
temp ra
connec thes elements Ai line ru from th transmitte
or npla
qu rement
maintenanc
ar show
lear nc
in ig 7.
spac is requir
im nsions of contro
.the, instrument-air header
Leve controller usuall have gage-glass companions
It
gl sses from he ontrol valv mani ol
he op at ng
than
prov economical Typica standard manifold ar show
[10].
outlet lo approa
th ontrol va ve om an leva io
ve se
he looped bypass type erve ho izonta
lo
structural columns.
On drai poin isrequired if th
ai
losed. In satu ted-st
trol-valv manifold.
he utom ti
ontrol va ve
ontrol valv
lo
pa
ails open
on or tw st am
of an inst um nta-
sizing pump-suction piping
References
1. "Handboo fo Contro Valv Sizing," Masoneilan International, Inc.
Norwood, MA 02062.
2. Dimensions-Masoneila
Contro Valves an Auxiliar Equipment,
Masoneilan International, Inc. Norwood, MA 02062.
3 . " Va lv e i zi ng ,
a ta lo g 1 0 i sh e
o n r ol s o .
a r h al lt o n , I A
50158.
4 . i sh e
o nt ro l
a lv e i me n i on s
u l e ti n 1 -1 00 , F i h e C on tr o
Co., Marshalltown IA 50158.
5. Boger, H.·W., Recent Trends in Sizing Contro Valves 23rd Annual
S ym po si u
o n I n t ru me nt at io n f o t h P r c e
I n u st ri e
e xa s
A&
niversity, Colleg Station, TX 77843, 1968
6 . B au ma nn ,
h e n tr od uc ti o
r i i ca l F lo w a ct o o r a lv e
Sizing,ISA (Instr Soc. Am.) Trans. Apr. 1963
7 . a um an n
. , f fe c o f P ip e e du ce r o n a lv e a pa ci ty , IllS/I'.
Control Systems, Dec. 1967
Instr.
Contro Systems, a n 1 97 0
9. Boger; H. W. Flow Characteristic fo Contro Valv Installations,
S A I n t r S oc . m ) 1., Oct. 1966
10. Hutchison, J. W. (Ed.), "ISA Handbook of Contro Valves,', ' Instru
ment Soc. of America, Pittsburgh 1971
93
Su ce sful operatio
of pump
characteristics. Reduce
suction.
Example. Fig.
potentia
conhave be
'-
bert
se ec ed
Available
rn
2:
and
8)
9) fo NPSH
Lines
50 It
raw- ff nozzle
izing.
45
and
f f ff f ff in f f i f f i : f : n : m : n 7 i ff E f f i
lJ~--I~
t-J:j:ffiti=~~~~-::j
K=O.78
h.i.
/2g.
3K .V2/ (2g)
Where
(0.408) Q/d
sistance coefficien K,
1.
hL
1.
vi
Fig I- Graph
for estimati
draw of
nozzle sizes
hi.
'v==:':
2.
EXAMPLE:
-.
:~~::~:;:::::G
um
__L_
-n
us
b e p :n : a b
he
amoun
Flow rate
2200gpm, hr
th
Pipe size:
v'O.4D8 Q/v
11 in.
Nomina size
Fig 2-Suction pip
15in.
7.4 [t./sce
' O. 4
.4
12in.
co nections
to .elevated draw-off nozzles.
iA3i.E2-r 1F' ~-a celc leticns form with th
lOr;: [;::91.3
Subcooled
Liquid
Saturated
3.
4. S ta ti c
(a
b)
h ea d
ine
5. L(+
p re ss ur e
(c
8.
6'
Line
~V/~'
at
10.
oess
Line
·_~psi
p re ss ur e
ti
no le
~~;i~;~~)
R eq ui re d
at
tota
of suctio
pipe re istanc
wn
Fig-
Flow Data:
iq id pu ped: Heav
as-oil
Fl
rat at te perature
00 pm
pecific gravity:
0,88
Density:
lb .r
ft
Viscosity:
.6
\1 inim
liquid leve in
ctio dr
i.
With ht.
18inc
th velo it fr
ctio
\10.40 (900)/8
6.78 inc
pipe
ad
iz
ni Fricti
Lo
Reynolds Number: Re
Lo
ti
10
ampl
18 in
1, II
ft./sec
800
in.,
Fig. 4-Manufac urer's
dule 40
NPSHdiag am
·s
should includ
yn ld
(900 /32,380)
and
ps
40
Total:
at ospheric
nd
flow th pressure
an
(a)
,-
45
gate valv (open)
strainer:
reduce (6-in.
tati
L in e
by
20"":
Equivalent
Line lengt
elb ws 3(22)
Eq ival nt
fo
50.6 (Q/d) (p/I')
50.6 (900/8 (55/0.6)
522,000
Moody's! diagra
at this
fricti
fa to fr
Number,
0.016
AP100 (8-in.)
1.35fS(Q2/d
1.35 (0.016 (0.8
0.47 psi/10 ft
Lin
= ( 3 , 5 '5 )1 /1 4
.fJ'7
\10.408 Q/
nozzle iz
No inal nozzle an
32,38 in.
Suction
al
pipi g.
(d
ti
p)/144
.\1.
i s n e ga ti ve .
PUMPV1
E-
N PS H
SUC!IO
R.F.
(
f
t
. head
co figu atio
ps
ft
.lQ§_)
NP
12"·/·
Fig. 3-Exampl
15
P_S~
ai
YM
6 -
ps
_ _
A va il ab l
~STRAINER
49
ps
Line
6.
7.
180/100
ad lo
acuufi-l
0.475
0.855
(144 psi)/p
(144 0.855)/55
.2 ft
re ures
line.
or subc oled-liq id
Piping-9). Pressure-S Pressure Drop-S Pumps-4, Resistance-S Size-7 Sizing-B
Suction-S, V np o
P re ss u re -S ,
~-
Iping
Intera ti ns betw
n" ydra li
requir
nt
an
piping
nfig rati ns
naf
il ar ty
it
ap
ip ng
ig is an
tial requir
nt fo th de igne
ydra li
yste
Th accuracy-of
is calculati ns predictions
flowrat
and pre re differentialc.reiiabiliry
f_ peration, and
th cono ycapitai, nergy,~aintenanc
an
peratin
ts pend to gr at
tent
pipe
nfig ra
ti ns an pipe co ponent
In th
article we av recogniz d. th importanc
raphic ipin
nd to
imit
re
av
pr nt
it fundam ntal
We will now. valuat th
fl
yste
nd piping
ig
is illati
ln,
isa
re in rate
it th
th in
id
al yste
discu
in
arlie article
Layo
ro
fo di tillatio
fl
a.'t pi
is il at
rac
.'
levation. Th
p-
ti
th
in
ip
ir
ti al run,
ip
an
towe nozzle belo
fr
with
ab
l-
am
line
lo
th
re
pipe rack
levatio is
an al
ne
ld
fo th
be arrang
lin
this le
ts
ip line
roppin
atio
ll appr
ip ra
by
ro
ip
li
bank
boil
is
le ti
te
is al
in
fo
ally
team
ne
to
(F/ 1)
th
inth actua. plant.
nd pl
awirig fo
th prin ipal leIil. nt
ally integrat
intoa.
acce aisle at
installations). Each IIlanh le
platformforIilaint nanc~. alve
an in tr
Fnts
locate above th
platform fo c6nv nient:atc
Fo
no y'a.nd asy·.s pp rt piping
ld
<iIllm diat ly
po leavin
th towern ztle
an
vertical line lend
tr ig
ni
ti
in
leav
.the
11).
lo at
ad ac nt to ac
in Fll,
fi
le ti
lu n.
di tillatio
lu
ar
le
colu ns
ia ra
li
it lf as
ific
itable lo ti
ri nta. t'
the towersh0\oVsthe segment
1s f.it
ir
ferenc
allott dt
.•piping no zl ,ma.n:
th
le ,platf rm
ra
nd la
patt rn
~'llfl llyl ad t? a·.w -organiz I<lrrang
ntfo
th
rpr
quip nt an au iliaty
ponent
as
ar
ro
ru
.".: q~alplatforIil7~r~ck tspacing
and'tJ J.eorientati0Ilo
br<tCi<etsline
al ng th
ntir length
th towet:
(T~i~. will inipiize interf renc
betw
th piping
.•
aJl. tr turalm bers;.
rdin to
HA,Jad rs
··... ~~t\
platfofIIl ~l1()u~d notb~) ng r· than t?Qft;
th
r~ ar
iJ il
tw
tf ad rs
id
th
ll le
ne pp a: in
atid
-
..
. '
\
()Jl.b th
th pi
ra
' : : i . ' . ; '/ ; " - . " .
~!;;! ~: ,.
(.,:~:::?:::-~;
Overhead lin
,I
,. Line with both ends higher
ineswith ne en
Distillation
column
elow
rack on either pipe
rac elevation
_L sw hb
ends lower than
e r
Condenser
-Access
to pump
Grade
Reflux pum
valv _/
...Alternat
suction line
suction'
b. Elevation
Steam
Pip rack'
-·-Downcomer
a..- Process
flow.diagram
:,-..
-',,-
t_
.
-,~-
_.
ca turn left
right, depending
the-plant's overall
arrangement.
di tillatio
lu n, th larg
line ar th
verh ad vap line and th reboile downc
and
return. Thes line sh ld ave the.simple and
st
direct configurations,to inimizepress relossand cost:
ring normal peration, th pu
in Fig, tran
ports liquid at quilibriu This
ans that th distillati n.colu
and reflu dru are levat d'to atisfy c.
NP H(n tpo iti~
ctio
ad) require nts Th
discharg linesofte have two destinations..Total-head
requirementssho ld be designedand calculated sothat,
perating points fall
th pu p's head-capacity curve
wh pu ping to an alternativ de tination. Alterna-,
ti di
ar linesca
av qual apacit an alternative peration,
partial capacity wit
im ltane
peration. All alternatives..sh ld be. investigatedf()l".
-,.
,;
_.
_.--,
thro gh towe nozzles,and extending acrossthe towe
.. dia ter. Reboilers wit
all at dutie are
ally
designe as helical coils
Reboilerarrangement~.
In
ri ntal th
yp
reboil rs liquid fl
fro an levated dru .· r·towe botto .oJ: towertrapo t,bo thro gh dO,W'nc
eripe.tOit~ebotto
exchangershell. Th liquid iSheated,.leaves'th re
,.,> Th de ign fo ~pu pe
rebo~lercirc it is
ilar..;·boil
th returnpipingas
ap r';liq id. ni ture
totll(1t
refluxpUInpsyste Ab tto pu
trans-.
and floW's,backi: th .tower()r drum..
port th liquid thro
;:
Ilger' fire
at
In vertical reboil ts
at lg
ally
th
an.clreturnsit to th distillatio colu n; Closeattenti0n.;
shellsid.e.Inh rizontal reboilers,beating is
th tube
90%
··.··.shCl~ldheaid to.possible.two-phase.fl9W'i n pipeline
id Fora larg vaporati
rate (f re pl
.._ '.co ing aft ,th
ater- peciallyw
we~~tt9;
totalfl.,?",),a k: ttl tYP9.r boiler, sed.;;/;';
'.i.
"'locate the.heater:clo etoth
~olurnn~..•..
Pii>ingto horizontahrebOilers'is de$iS'll9d:~s
'..: In rt d-type reboil rs av n,
pr
·pipin ~·
and' dire tly: 3.$.po iblew~thin th litnitatipns
.· 'L
r-diam te tow9rs.can av pn to fo rU-t b,
th rmal.. pansion.forc ........
"\........
.:'stil.bb,llndle ins rt~~',?Jrectly'int t~Jiq i4.~pace
.S rn1lWtricalr rang
ntsbetw n.th .dJ;aW'off
;~i': ' _ " ; - ; : \ / ~ ' 2 : ~
il
tl
inle no le as
an return conn ti
nons
pt
.~~
ic
piping
nf
re-e no ical
fo
bo le
as be we
th rebo le
th tower, ar pr ferr
ft
av
trical piping an atte pt
th
re istanc thro
re re istanc in
in th
th r. Henc
in
bo leran
nozzle
atio
ay ls be ac
re-fle ible piping
tl
an
ld be
tw
ad
pa alle
to qualiz
both le
th reboil
piping
ne le pr duce
alle fl
than
neve
at di trib ti
will
nt
il be
gravity-fl
bypa
is
Maximum
liquid level'
ally pr vide
Steam condensate
a. Bottom of reboiler should be elevated just abov to of
condensat pot
--Distillatio
fr
column
comer.
alve ar
rarely in lude
in re
il
piping
pt
th
bo
ar
an
pe at
at an
wide
at-capacit
rang
co pani
requir line
blinds to blan
ff th towe no le
ring
td wn
turnar nd an
aint nanc
conn ct to th tube id
rizontal reboil rs Th
quir
reboiler'
ar an
Reboile
tube id
no al
inl t.
ad
inle
ar
1:
elevations
bo
nt line le at ns
ab
ab
nd
leve fo
changers ab
at gr~d provid
cono ical arrangements=-valves.arid
nv ie t, an
aint nanc
as
ar an
nt th tati
ad ar well determin
betw
th
xc an r'
nt rlin an th draw ff and.return nozle
ti al re il
an
al
pport
th di tillatio
lu
it lf
reboil rs
po lo at
aftert
lr
as
what
th
ig
av
nd nsat or.Iiquid-holding
tube id
tl t,as
wn inF-
nt rl ne le at
an
nits
at
F!
trap
to
th
nd ns
po
than th bottom
th
xc ange
ng
be
th
nd nsat an
th
xc anger'
at-transfe duty
nd nsat le l.in th reboil
rang
eat-transfe control.
in th pr is relati ns ip
'>and:thevertical
..condensate-c
th
no
reboiler
av
ld no behi
ll to av id floods'
ad
affecting'
r,to pr vide fo awid
Pc.fPce sonditions.deterbetw
th
an
ntrol·p()t·
rf't,niiif'Y"
h:o.
UH<:;Ul<:;l;'V.Jl
centrifugal
th
le~e inth
xc an
r. Th
H:'VdUlJ,1
dirrerence tOlm~:n7:'
Required elevation
difference betwee
liquidJevel in tower
and exchanger
th
Ut
th
R e e re nc e
l in e
tl;
3.5 to 5.5 ft
0:
a. Horizonta
Liquid density in downcomer
P2' Liquid-vapo mixtur densit in rise
Pl
P3:(Pl+P2)/2,
Averagedensity in vertical reboiler
Horizontal
io H1in F/3) pr vide th po itiv -stati
ad fo
flo in the reboiler circuit, and verco esfrictio losses
in th xc anger, an down
an return line •.
Designin
th
icaUyin F/4.
am at th tower'
il
tl
yste
an
return no zl
ir
referenceline.and
isbackpressure in the riser'svaporliquid colu n; th pressuredifference (tli'=P
.m st verco
the exchange and piping frictio losses
,!Th refore
1m
be gr at than
1i th
/144=
liquid densityin th down
r, th
,can
tw alte nati
.;.' '>
.,.c..
1.
rizontal
'lahtioni~,.forced' by the static-head differen.cebetweti~.·.·r:,.,.".,'.,·.,.'".",.,,'.,.
t,
.·
liquid colu
in th riser Fo convenieri:ce,referenc~wher
lin are ch
at th xc ang r's centerline fo
J:i~
'zontaLreboilers and at th botto tube ee forverti~i:
calreboilers.'Xi<
.~_",
If-,::_ft·""iS:,Jiquid,
t he ' " -d .o w n co m e r a t : . - ~ . ~ , t h ~ ~ : : , > ':,.,.
an
rs (s
rtical
an
(pzH
where
th
P3H3)/144,
ai
ra
it
F/4b and F/4d):
rs (s
ix
ity,
iq id an
re
iq id-v
ixtu
in
4,000
3,000
(4)
2,000
reboiler:
Eq (4 provide
cons rvative
timate
ra ient in
rtical reboil rs
tual
nsit
q..
1,500
th density
il be le
'"
th vertical reboil
ld be Ho ded.
axim
levati
th to tube
ld no be ig
than
th
in
liqu
le
th
Hydrauli
in
ri
1,000
800
.Q
'-$'
600
400
300
.u
ntal reboil rs ,.
In th following di cu ion, th
ydraulic conditi ns
nl in
rizontal
an rs
il be de loped. (T
derivati ns ar th am fo vertical exchangers.zexcept
that
will replace
riz ntal xc ang rs
:) Fo
I If
af ty fa to
re diff renc
pr
(5
AP
isintr
fo fricti
lo
th
th availabl
is alved, and:
(6)
quantity (H
ly
ni
ri in
fo
3 / 8 8 )P l
.OIP is always availabl
exchangers
14a).
Th
in
at:' horizontal
depends
im
le ivin fo
th
le ti
iffere
th
ra
le
xchange centerlin (di nsio
ap rati
taking plac in th reboil r.
le ting th
vapor-c lu
backpre re in th return lin ,th ax
im
able ri in forc is
(7)
ap li atio
th
belo this
axim
th
tower. Fo th
APmaz
al
iv ng fo
is
lu
to
ally larg
Frictio
an
inac
ll
av ilab
than al late
lo
ra
isw
pe iz
pipe ia ters
re
r-
,,
in reboilers
to al fric io lo
l- rc la in
boil
yste
be
alle than th availabl drivin
by fricti
forc Th pre re lo ca
ta
plac
in tw
ai lo ations in th
an
it lf
,and
in th
piping
.\
Hence:
APp<AP
values':
0.02Pl
Shaded part of char establish'e size of downcomer.
Frictio
as ,O
lo
in reboilers, A P e ' ar
nerall
ps (A note
ld indicate .w
.
to 0 . 0 8 P l
.
ractions
iv
th
'1
. 100 t.
Chern.Eng., Jan. 6,1975
'I
. ·••.
12
ft, and
APma
50,lb/ft
1 2 8 8 )5 0
impl
relati ns
orationnite
is
ps ar
.1
2.0 PSi;~ia~dl:e~:~B~l~~~:~~~!::r~~~~:~~!~P;:~:<!n~~;~tl
ful.
th
ap
.. ,e Fi
av
1' ....
di
rPl::rralt_.
n)d'
erro '.ca·.··
.•l··.c·u·
la·
..•
···I:o.ns,. ·...ec
.···t··
e . is pr
le
tha. .1,P.m J:
'altlPmdzk.as
oat
APmaz'
However,even
nt
1.·..
..•..
in F/5'T is'\
....
evaporation.
>p
if
'a
...•..
jt.•.....
"<.11;
nd
In vertical reboil
nd
forc
an be
rate ar
ig
turn line is
circ it re
an
il
lo
ar
le atio
th
in
HI>
le ation,
at
th
nc
(6), where
Q, from:
fl wrat
5,000/500(36.7/62.37)
with
rawoff no le
late volu
Q= W/500S
gr at r,
d. In
ttle-typ reboil rs
vaporati
Fo th
reboil rs
larg -dia te
ally nece ary.
we al
imilar co putati ns
28 gp
fo th
ri r-re
bering
reboil
line
putati ns fo ch
in wh th
th
line iz ar ad quat
requir
nsid rabl
detail
ld al note that th
boil
as wo inlets an
F/
3, ft:
(9
3P
PI
wn
replaces .P
co r, ri
an
P2
no le anno
xc ange
I::!.p
I::!.p
I.
be lowe than
requir
th
nt
I :: !. P d + I : :! .P r
re
ally
il r'
au
inim
I::!.Pe
th
pr
ve
levati n.
nstrate
an
th
is in reas
th
Viscosity,
Molecula
(hot)" p, Jb/ft3
}L, cp
weight,M
ti n,
al
85,000
36.7
0.6
Liquid
Vapor
59,500
36
0.5
'25,500
1.31
0.01
53
,,_--',.p.:u
= M
--"-'-,,
53(181.7)/(10.72)(6 2}
:;:;=.-
-'--
1.311b/ft~;
le
nold
nu be
fr
Re
ac
ar
ar
(Chern. Eng.,
ni
lo
fr
I::!.h~o
I::!.PIOO
0.0216(0.0182)(36.7)[(289)2/6,346
LlPlOO
0.19 psi/IO
'Nile
0.5(155,3'00
0.021Wh(Q2/d
.W no
termin
fittin
fo
ac
series (ChemEng.,
th
nt
ft
.;.. 77,6~0;f=
psi/l0
ft
·.·.26
18
lo
10
30
36
Total
pipe an
Segment fo
lOO Flow,
Flow
.:.'.Ac.tual length
'(jyer'ill
0.02
quival nt length
ro
tables-inPart
Ft
*Oneelbowfo
0.022
as follows:
50
.Elbows
Sharp tee
,E
lo
density,
th
50.6(Qld)(p/JL)
Re
,·Entran
'-'-':"'~
late th
(50%)--_ 0.19 (- 144. )2
Riser,
Liquid
Density
calc lati ns
in
lO (50% 0.0574
Downcomer
Ib/h
de ig
,3
calc lations
F/
Flowrate;
affe ts
I.D.
-especially wh re large-diam te lines are nece ary.-Un,ec no ical reboil
line ar ju carele ly versiz
po rly ro ted.
Example de
nt
in fr
is
fu wh
el vatio adj tm nts
ig ts during raphic piping de ign,
be
at
at
coefficient fo P2
betw
th downco
an ri
no le If
an
ns
ti n.
diff renc
arrang
Downcomer-For
fricti n-lo
al
ad to ve
ar
fl
20
82
50%flow $egment;2 fo 100
pr
relo .o
th
nc
r:
' A P : :; { ) .1 9 ( 6 4 / i O ) . f
Dec. 23 1974 pp. 58-66 fo co~plete
Hence:
D.Ptoo(50%)
te
50
100% Flow,
Flow,
Actual length
18
Elbo
24
nt an
lo
24
48
Total
68
verall pr
I1
re lo
th
1.01(80/100)
ri r:
0.34(68/100)
downcomer,
.a
1.04 ps
ri
an
in
reboil r:
7 p
..
..
Total
fo this
Riser-Since th
le
pipe
0.3474Jt
ti n, we
NI
is
-i
ip
.P
le
late th
ap r-phas
yn ld
NIle
tain
fricti
D.PlOo
0.000336(fIPv)(W
D.p!oo
0.000336(0.014/1.31)[(25,500)2/32,380]
D.p!oo
0.072 psi/IO
-.
availabl
re
pr
ifferenc
re lo
sa
_'
.
."
.~,,,:._
pr
re
1.57 ps is reat
1.55 psi. Th re
te li
th
il
15.5 ft
nozzle is actuall
ft
15.55 fyis~sceptable.<.
ti le in this
ie will
ic
pipeline fo th
ydra li an th rmal
curring in verh ad cond nsing yste
Id
Iliq idfl
ftowm dulu
pr
late
inc th draw ff
fa
ft
in
th
is
ndle
no determine th two-phas
th
288(1.535)-3(4.05)
0 .0 1
10
ld
termin
ff
le
th
b'1itituting into Eq. (9):
WvldfLv
= 6 3 1 2 5 5 00 ) 7 .9 8
we
ps
(1/288)[(36.7)(13.5)
availabl
than th
al
J.D.
al
NIle
this
wn
tu
ampl
1.55
th
in th
nditions
',.,:'.
fr
'jJ""t<"'""
hvdraulic-svstems design
and
nu be
the- a ut ho r o f
fields, a n h a t au g
fo th design of proces
layout graphi piping an
•~
W. K el lo g
was associate
C o i n E ng la n a n
.•mecnamca engineerin from th
._ ._ ..
U ni ve rs it y o f B u a pe st .
.•...
.......•....•.
t.
ad
Th
equipment ar
param ters fo Ineeting
li
istill ti
li
th
th
to
ipin
ic
ta li
ti
th
ig
th
Hoff
.,
ravity-flo
reflu
Horizontal condensers-
lo
circuits.
II
12.
type of condensation
offers
wide ange of clas ificatio
Th
lIb, vapor
tatic- ea
pres ur
difference
.P
II
(1)
.p
to
ce
D . p e ; and
Chern.Eng.,
es
if
D.pcv:
th
(2)
following:
Two-stag
th
condensation
Eq.
(3)
lation.
ch
ip
ipin
"F
io ap
th r,
Cbem. Eng.,
1975.
densities, p, in lh/ft"; an
inimal
1 13 .
CHEMICAL ENGINEERIN
SEPTEMBE
15 1975
dimensions
-fJh
Pr
~~t
f"=~*~J"<t~i',.~)<F,,,"'~;;!'=~~:!.~.-c;::.
To
COO~~i
Poin
e. Baturate
liquid {sheiiside condensation
a.
atuf3t8
Vapor
nerally, in
nd nsin
yste
th
ni lo
in th
psi/lO ft. Inle an
tle re istance to pr ce
quip
nt
ally take
nsid rabl portio
th pipeline
re istanc an
ld no be ignore in th calc lations
re
th
ti
is
unusual.)
In
riz ntal cond ns rs cond nsatio tak plac in
th
ll
is give lowe re istanc than th tube id
baffle (o baffle in th xc ange is in th
rizontal
plan thro gh th
xc anger'
nt rlin
If ne
ary,
tw inle an tw
tl nozzle an alv. th tota fl w,
an
redu
th
metrical.
ntranc
in
an
xi re istanc
le
nsid rably.
F/
co le
tr
before
fo F/l
torag
ll
ir
fl
th
130
CHEMICAL ENGINEERIN
SEPTEMllI~
15 IY75
Contro valv
in th
leg (Z
ld be lo at
at
return' li
an pr
tr
fficient tatic
ad before th valv inle will pr vent
vaporizati
acro th valve
pr duct co le
ld
no re iv
liquid-vap
ixture
fo these condensers
Verticalcondensers-Arrangements
with
it -flo
tl ts
in F/2
nd
svsicms
im nsio
in F/3), th
dimension ZI is
alle
ipin
ig
2' an
than
th
lo
al lo
isidentical (fo xa pl
fl w) li id
ip
intermittently th
nd ns will no
afte th
an
ld be
pr
re
with gr atly
th
l;
perate well
Zl
(F/2b).
ingle-pas vertical condenser is
re itable
fo liquid
bc ling than
ri ntal ne
al
lo
ig
an be adju te within
reat rang than
with
rizontal
nd ns rs (F/ ). Th requir
liquid
than
as
(see F/3a).
larg
ia
te
F/
than th
th
ravity-flo
refl
id
line
th
changer's designer.
Th
ydra li balanc
F/
(1/144)(H
fo th
P'2)
arrang
nt
1/144)H
al lo p.
th
ar
nt (F/3
lo
li
is an be pene at redu
nd nsat fl
to
th
lo
fill
it li id With this type
ting th pres re differenc acro th vent valv
ld
ti
points
th
nt line to lo ations wh re pr
re ar
pe te to be ab
qual
wn
(4)
.P
"here .P
exchanger, 6.Pe'
.P
"and
ntrol- alve (i any) 6.Pcv, resistances:
.P
betw
le il
.P
!::"Pe
(5)
6.pcv
le atio
ifferenc as xpre
fr
q. (4),
th
nd ns r'
tl
an th reflu inle noz-
where
is th
av ra
nsit
densit
nd nsat
in th
in th
rtical
an
refl
verh ad line fo
ydro arbo
di tillatio
F/
piping is th re lt
th th rm ip
ff
in ra
ity-refl
nd nsation. Fo th yste
wn in F/4
line
is
fl
In
it -flo
nd
In .t
arrang
eads), act al pre
the calc lations
reversal
in
pu
whic
tu
th
th
nt
tati
into
r:
(7)
eal lo p. prevents flo
arrangements
Typi al
(6)
1446.P)
th
Pu ped-reflu
te
lo
nt (b id th
re difference
.P
al
(8)
is
F/
nd ns r'
tl
an
/2
If th
ra ity-fl
line This lo
refl
an be
line terminat
fo
in
ld
F/
diff renc
rtical
where
will be
(9)
isus all
131
C m ;I I1 1C A L E NG [N EE IU N
S EP TE MB E
1 5 1 97 5
vapo density and
is vapor-liquid
i : · _ ~ . Th
simplest overhead
line g!V8S the
srnaitest pipe SiZ9.
in
bc ol
the
li id
g:"avit'/-frovoJ
cutlet line
Eq
D..P
8)
!:lP
!:lP
(10)
!:lP
{lSt
ab ve
drum.
backpressure (P2H2)
pressure difference betwee
(2) the
lower
h",;ld ((';Ii
Il
static-head
greater
vapor static
greater the condclIs;] tion,
greatf
tive
course
bad.pn',.sul'e.
P2H2 be omes po i-
ir«
()lllJc.ll'
outlet
-l
Eq. ( 1 ( ) sll()\\'s
ystem. This rnus:
i ( lus'c's. D.l'p, an
exchange
re ista ce
!:lPe:
(11)
!:lpl'
ranges
!:lPe
rWlwecn
frorn
0.:) to
psi.
The maxiruu
possible condenser-centerline
belo th l~cflllXdr
(dimen io
calclllakd froru h .
p}J
'Dim nsiona
relation
fo
!:lP
cond nser at grad
132
CHl~MICAL ENGINEERING SEpTlilllER 1 \ I !! '/ '
pp
D.pe)
location
Frot
flo
PI
re
sider:
th
rh ad
ap
line an be negl
te
n-
Expressing
=::
In layo
ir in ac
tive
ti
levatio
(144/P2)(M
de ign,
rdan
ad
fro
lu flo
ally th refl
dr
it th requir
th refl
pu p.
F/5
is le at
(n
iim nsions
grad
is nd
fl
(13)
an
irable
lo
F/
in th
ns
\J
surges.
sl g-flo
.Li
region.
)I/2,
133
C HE M C A
E Nf i N EE R N G
S EP TE MB E
1 5 1 97 5
th
velo it
(cal
late
with tw
72·i
dis.
overhead ·!!n:;-
'-.
tn";',,
>7'L21,,,,"
\~~~
di
~_.-,-'P:=
al
an
iChcm. Eng. June
ap
as ar
23,1975, p. 14 ), lo re io
in F/6 ar al
availabl fo vertical fl ws
th
ap
th
ap r-phas
an liquid-p as
lo ti
ar
nt
ti
tablis
th
ne al
ak
in th appr priate
fl
regi n.
it ri
fo
le ting
ar
il tv
th
th
po ible
it
bu
no
Equipmellt
~l'q\~l~d,
1',1
I.
EN(;INI:,i:,I;'INi;SlJ"II:~lIillt
al
(c
in
Il wrat
avit -II'l\
ll ranu
nt
LIIIOI.'. th lI,inll ~nce la;o
Iki()\\
I'"
al
an
alte nati
(el) changing
arrangement
:H
CIlEMICAL
ill ihe
H,l\{;II,,',·
al1d ldlw. dillin,
pipe run-. fIJI ;tll''1II;ltivc
to
gravltv-Illl
;ULlll
to
by (a incr asin
nd ns r'
le line an
(';11) be minimize
jii<)\'idilll;
dClS('f
itable line iz
ar
l«:
systt·lll. Ih,
II
av
ay
dl<>P
pn'ss\j!('
!'Cdu('ille;
F/6
ia ra
fl,,\\
t'l;',
tr tu
is
de ig ar
te
wn