lp-gas serviceman’s handbook
TRANSCRIPT
LP-10
LP-GAS SERVICEMAN’S
HANDBOOK
50
LP-GAS SERVICEMAN’SHANDBOOK
The Fisher Controls LP-Gas Serviceman’s Handbookserves as a general reference of information on LP-Gasand for the installation, operation and maintenance ofLP-Gas equipment. It provides key data and answersimportant questions that are relevant to managementand field servicemen in the LP-Gas industry.
Users of this handbook should consult applicablefederal, state and local laws as well as pertinentindustry regulations, including National Fire ProtectionAssociation (NFPA) Pamphlets No. 54 and 58.
Fisher Controls shall have no responsibility for anymisinterpretation of the information contained in thishandbook or any improper installation or repair work orother deviation from the procedures recommended inthis handbook.
For additional copies of this handbook please contactyour local Fisher Distributor, or call 1-800-558-5853, or1-319-378-8673.
1
Table of Contents
PROPERTIES OF LP-GASES ..................................... 2
VAPOR PRESSURE OF LP-GASES ........................... 4
DETERMINING TOTAL LOAD ..................................... 5
VAPORIZATION RATE ................................................. 6
CYLINDER AND TANK MANIFOLDING ....................... 9
CONTAINER LOCATION AND INSTALLATION ......... 11Container Preparation .................................................... 15
PIPE AND TUBING SIZING ....................................... 18Sizing between 1st Stage and 2nd Stage Regulators ... 23
Sizing between 2nd Stage Regulator and Appliance .... 26
2 psi and CSST Capacities ............................................. 28
LP-GAS REGULATOR INFORMATIONRegulator Selection ........................................................ 32
Two-Stage Regulation .................................................... 35
Regulator Installation ...................................................... 36
Leak Testing Methods .................................................... 39
Regulator Inspection ...................................................... 41
Troubleshooting Domestic Tank Fittings ........................ 43
LP-Gas Orifice Capacities .............................................. 45
Line Sizing Chart for Liquid Propane ............................. 46
CONVERSION FACTORS ......................................... 47
FLOW EQUIVALENT CONVERSIONS ...................... 49
TEMPERATURE CONVERSIONS ............................ 49
© Fisher Controls, 2001, 2005
2
APPROXIMATE PROPERTIES OF LP-GASES
1elbaT ENAPORP ENATUBalumroF C3H8 C4H 01
F°,tnioPgnilioBlaitinI 44- 13diuqiLfoytivarGcificepS
F°06ta)0.1=retaW( 405.0 285.0tadiuqiLfonollaGrepthgieW
BL,F°06 02.4 18.4,diuqiLfotaeHcificepS
F°06taBL/UTB 036.0 945.0repropaVfoteefcibuC
F°06tanollaG 83.63 62.13repropaVfoteefcibuC
F°06tadnuoP 66.8 15.6ropaVfoytivarGcificepS
F°06ta)0.1=riA( 05.1 10.2F°,riAnierutarepmeTnoitingI 021,1-029 000,1-009erutarepmeTemalFmumixaM
F°,riAni 595,3 516,3otderiuqeRriAfoteefcibuC
cibuCenOnruB saGfotooF 68.32 20.13,riAniytilibammalFfostimiL
:xiMsaG-riAniropaVfo%rewoL)a(reppU)b(
51.206.9
55.106.8
tanoitaziropaVfotaeHtnetaL:tnioPgnilioB
dnuoPrepUTB)a(nollaGrepUTB)b(
481377
761808
retfAseulaVgnitaeHlatoT:noitaziropaV
tooFcibuCrepUTB)a(dnuoPrepUTB)b(nollaGrepUTB)c(
884,2845,12205,19
082,3122,12230,201
3
APPROXIMATE PROPERTIES OF LP-GASES
Table 1 (Metric) PROPANE BUTANEFormula C3H8 C4H10
Initial Boiling Point, °C -42 -1Specific Gravity of Liquid(Water = 1.0) at 15.56°C 0.504 0.582Weight per Cubic Meter ofLiquid at 15.56°C, kg 504 582Specific Heat of Liquid,Kilojoule/Kilogram at 15.56°C 1.464 1.276Cubic Meter of Vapor per Literat 15.56°C 0.271 0.235Cubic Meter of Vapor perKilogram at 15.56°C 0.539 0.410Specific Gravity of Vapor(Air = 1.0) at 15.56°C 1.50 2.01Ignition Temperature in Air, °C 493-604 482-538Maximum Flame Temperaturein Air, °C 1,980 1,991Cubic Meters of Air Requiredto Burn 1 Cubic Meter of Gas 23.86 31.02Limits of Flammability in Air,% of Vapor in Air-Gas Mix: (a) Lower (b) Upper
2.159.60
1.558.60
Latent Heat of Vaporization atBoiling Point: (a) Kilojoule per Kilogram (b) Kilojoule per Liter
428216
388226
Total Heating Values AfterVaporization: (a) Kilojoule per Cubic Meter (b) Kilojoule per Kilogram (c) Kilojoule per Liter
92,43049,92025,140
121,28049,14028,100
4
VAPOR PRESSURE OF LP-GASESVapor pressure can be defined as the force exerted by agas or liquid attempting to escape from a container. Thispressure moves gas along the pipe or tubing to the appli-ance burner.
Outside temperature greatly affects container pressure.Lower temperature means lower container pressure. Toolow a container pressure means that not enough gas isable to get to the appliance.
The Table below shows vapor pressures for propane andbutane at various outside temperatures.
-AREPMETERUT
ROPAVETAMIXORPPA2ELBATGISP,ERUSSERP
ENATUBOTENAPORP
F° C° 001 % 02/08 04/06 05/05 06/04 08/02 %001
04- 04- 6.3 — — — — — —
03- 4.43- 8 5.4 — — — — —
02- 9.82- 5.31 2.9 9.4 9.1 — — —
01- 3.32- 02 61 9 6 5.3 — —
0 8.71- 82 22 51 11 3.7 — —
01 2.21- 73 92 02 71 31 4.3 —
02 7.6- 74 63 82 32 81 4.7 —
03 1.1- 85 54 53 92 42 31 —
04 4.4 27 85 44 73 23 81 3
05 01 68 96 35 64 04 42 9.6
06 6.51 201 08 56 65 94 03 21
07 1.12 721 59 87 86 95 83 71
08 7.62 041 521 09 08 07 64 32
09 2.23 561 041 211 59 28 65 92
001 8.73 691 861 731 321 001 96 63
011 3.34 022 581 561 841 031 08 54
5
DETERMINING TOTAL LOADThe best way to determine BTU input is from the appliancenameplate or from the manufacturer’s catalog. Add theinput of all the appliances for the total load. If specific ap-pliance capacity information is not available, the Table be-low will be useful. Remember to allow for appliances whichmay be installed at a later date.
If the propane load in standard cubic feet per hour (SCFH)is desired, divide the BTU/HR load by 2488 to get SCFH.Conversely, the BTU/HR capacity can be obtained fromSCFH by multiplying the SCFH figure by 2488.
Figuring the total load accurately is most important becauseof the size of the pipe and tubing, the tank (or the numberof cylinders), and the regulator will be based on the capac-ity of the system to be served.
Table Reprinted From Table 5.4.2.1, NFPA 54, 2002 ed.
TABLE 3 GAS REQUIRED FOR COMMON APPLIANCES
APPLIANCE APPROX. INPUT BTU/HR
Warm Air Furnace Single Family Multifamily, per unit
100,00060,000
Hydronic Boiler, Space Heating Single Family Multifamily, per unit
100,00060,000
Hydronic Boiler, Space & Water Heating Single Family Multifamily, per unit
120,00075,000
Range, Free Standing, Domestic Built-In Oven or Broiler Unit, Domestic Built-In Top Unit, Domestic
65,00025,00040,000
Water Heater, Automatic Storage, 30 to 40 gal. Tank Water Heater, Automatic Storage, 50 gal. Tank Water Heater, Automatic Instantaneous 2 gal. per minute Capacity 4 gal. per minute 6 gal. per minute Water Heater, Domestic, Circulating or Side-Arm
35,00050,000
142,800285,000428,00035,000
Refrigerator Clothes Dryer, Type 1 (Domestic) Gas Fireplace direct vent Gas log Barbecue Gas Light Incinerator, Domestic
3,00035,00040,00080,00040,0002,50035,000
6
VAPORIZATION RATEThe rate of vaporization of a container is dependent uponthe temperature of the liquid and the amount of “wettedsurface” area of the container.
The temperature of the liquid is proportional to the outsideair temperature and the wetted surface area is the tanksurface area in contact with the liquid. Therefore, whenthe outside air temperature is lower or the container hasless liquid in it, the vaporization rate of the container is alower value.
To determine the proper size of ASME storage tanks or theproper number of DOT cylinders for various loads, it is im-portant to consider the lowest winter temperature at thelocation.
Multiple cylinders or tanks may be manifolded to give therequired vaporization capacity. Withdrawal of gas from oneor two containers can lower the container pressure sub-stantially due to the refrigeration of the vaporization gas.Regulator capacity is then reduced because of the lowerinlet pressure. Where any reasonably heavy gas load isexpected, put sufficient cylinders on each side of an auto-matic changeover system.
See pages 7 and 8 for more information.
7
VAPORIZATION RATES FORASME STORAGE TANKSA number of assumptions were made in calculating theBTU figures listed in the Table below:
1) The tank is one-half full.
2) Relative humidity is 70%.
3) The tank is under intermittent loading.
Although none of these conditions may apply, the Tablecan still serve as a good rule-of-thumb in estimating whata particular tank size will provide under various tempera-tures. Continuous loading is not a very common occur-rence on domestic installations, but under continuous load-ing the withdrawal rates in the Table should be multipliedby 0.25.
)RH/UTB(etaRlawardhtiWtnettimretnI.xaM4elbaTroodtuOtsewoLfi*gnitsorFknaTtuohtiW
...sehcaeR)sruoH42roFegarevA(erutarepmeT
ERUTAREPMET)SNOLLAG(EZISKNAT
051 052 005 000,1
F°04 009,412 001,882 008,874 008,258
F°03 009,781 008,152 006,814 006,547
F°02 008,161 008,612 004,063 009,146
F°01 000,841 004,891 007,923 002,785
F°0 007,431 006,081 001,003 005,435
F°01- 004,231 004,771 008,492 004,525
F°02- 008,801 008,541 003,242 006,134
F°03- 001,701 005,341 006,832 000,524
.etarnoitaziropavehtgnicuder,rotalusninasastcagnitsorfknaT*
8
Vaporization Rates for 100 PoundDOT Cylinders“Rule of Thumb” Guide
For continuous draws, where temperatures may reach 0°F,assume the vaporization rate of a 100 lb. cylinder to beapproximately 50,000 BTU/HR Therefore the:
Number of cylinders per side = total load in BTU/HR / 50,000
Example:
If a total load requirement of 200,000 BTU/HR is to be sup-plied from 100 pound DOT cylinders and winter tempera-tures may drop to 0°F, then how many cylinders are neededper side?
Number of cylinders per side = 200,000/50,000 = 4
* When using a changeover regulator, 4 cylinders perside are required.
Vaporization Rate Table for 100 Lb. DOT Cylinders
ELBAT ROFHUTBNISETARNOITAZIROPAV5SLEVELDIUQILDNASERUTAREPMETSUOIRAV
FO.SBLENAPORP.LYCNI
F°02- F°0 F°02 F°04
001 000,56 000,17 000,97 000,49
09 000,06 000,56 000,27 000,58
08 000,45 000,95 000,66 000,77
07 000,84 000,25 000,95 000,96
06 000,34 000,64 000,25 000,16
05 000,73 000,04 000,54 000,35
04 000,13 000,43 000,83 000,54
03 000,62 000,82 000,13 000,73
02 000,02 000,22 000,52 000,92
01 000,51 000,61 000,81 000,12
9
CYLINDER AND TANKMANIFOLDINGOften it is necessary to manifold cylinders or tanks to ob-tain the required capacity needed for the installation. Mul-tiple cylinder hookups are most frequently used on com-mercial applications and at many residential jobs, eventhough tank manifolding is common in certain areas.
On certain multi-cylinder or tank installations, an automaticchangeover regulator can be used. These regulatorschange from the supply cylinder (when the gas is ex-hausted) to the reserve cylinder automatically without hav-ing to shutdown the system to refill.
A typical cylinder manifold using an automatic changeoverregulator can be installed in line with multiple cylinders.(See Figure 1 below.)
Figure 1
AUTOMATIC CHANGEOVERREGULATOR
SCH 80 1/2-IN PIPE MANIFOLD
COPPER PIGTAIL
10
CYLINDER AND TANKMANIFOLDINGWhen manifolding cylinders or tanks, do not use a regula-tor at each container. When this is done, the required ca-pacity for the particular installation may not be obtained. Itis impossible to set all of the regulators at the same outletpressure. The regulator delivering the highest outlet pres-sure will backpressure the other regulators, keeping themfrom operating. In effect, only one container would be sup-plying gas in this sort of situation.
The answer on manifold installations is to run high pres-sure piping from the containers into a common line, asshown in the Figure below. Then, install a regulator thatcan handle the required capacity. Two-stage regulation isthe most effective system on tank manifold installations.
Figure 2
2nd STAGEREGULATOR
Schematic of atank manifoldinstallation
1st STAGEREGULATOR
11
CONTAINER LOCATION ANDINSTALLATIONOnce the proper size of ASME storage tank or the propernumber of DOT cylinders has been determined, carefulattention must be given to the most convenient, yet safe,place for their location on the customer’s property.
Containers should be placed in a location pleasing to thecustomer that does not conflict with state and local regu-lations or NFPA Pamphlet No. 58, Storage and Handlingof Liquefied Petroleum Gases. Refer to this standard todetermine the appropriate placement of LP-Gascontainers.
In general, storage tanks should be placed in an acces-sible location for filling, supported by concrete blocks ofappropriate size and reinforcement, and located away fromvehicular traffic.
Cylinders should be placed with ease of replacement orrefilling in mind, secured on a firm base, and protectedfrom vehicular traffic, animals and the elements.
For both ASME and DOT containers, the distance fromany building openings, external sources of ignition, andintakes to direct vented gas appliances or mechanicalventilation systems are a critical consideration. SeeFigures 3, 4 and 5 on pages 12, 13 and 14.
Refer to NFPA No. 58 for the minimum distances that thesecontainers must be placed from the building or other ob-jects.
12
CONTAINER LOCATION (cont)
Cyl
inde
rs n
otfil
led
on s
ite
3-ft
Min
.
Inta
ke to
dire
ct v
ent
appl
ianc
e
Cra
wl s
pace
ope
ning
,w
indo
ws,
or e
xhau
st fa
n
Cyl
inde
r fill
ed o
n si
tefro
m b
ulk
truck
10-f
t Min
.(N
ote
2)C
entr
al A
/Cco
mpr
esso
r (so
urce
of
igni
tion)
3-ft
Min
.
5-ft
Min
. (N
ote
1)
Win
dow
air
cond
ition
er(s
ourc
e of
igni
tion)
Not
e 1:
5-ft
min
imum
from
relie
f val
ve in
any
dire
ctio
n aw
ay fr
om a
ny e
xter
ior
sour
ce o
f ign
ition
, ope
ning
s in
to d
irect
vent
app
lianc
es, o
r mec
hani
cal
vent
ilatio
n ai
r int
akes
.
Not
e 2:
If t
he c
ylin
der i
s fil
led
on s
ite fr
om a
bul
k tr
uck,
the
fillin
g co
nnec
tion
and
vent
val
ve m
ust b
e at
leas
t10
-ft fr
om a
ny e
xter
ior s
ourc
e of
igni
tion,
ope
ning
sin
to d
irect
-ven
t app
lianc
es, o
r mec
hani
cal v
entil
atio
nai
r int
akes
.
Figure 3 Cylinders
Rep
rint
ed fr
om N
FPA
58
Fig
ure
I.1(a
), 2
002
ed.
(1 ft
= 0
.304
8 m
)
13
CONTAINER LOCATION (cont)
Rep
rint
ed fr
om N
FPA
58,
Fig
ure
I.1(b
), 2
002
ed.
Figure 4 Above Ground ASME Containers
5-ft
Min
.
25-ft
Min
. (N
ote
2)
10-ft
Min
.
10-ft
Min
.
Cen
tral
A/C
com
pres
sor
(sou
rce
ofig
nitio
n)
Cra
wl s
pace
open
ing,
win
dow
s, o
rex
haus
t fan
10-f
t Min
.(N
ote
1)
5-ft
Min
.
125-
500
Gal
. w.c
.Und
er 1
25G
al. w
.c.
Inta
ke to
dire
ct v
ent
appl
ianc
e
10-ft
Min
. (N
ote
1)
10-f
t Min
.(N
ote
1)
25-ft
Min
. (N
ote
2)
Und
er 1
25 G
al. w
.c.
Win
dow
air
cond
ition
er(s
ourc
e of
igni
tion)
Nea
rest
line
of a
djoi
ning
prop
erty
that
may
be
built
upon
(1 ft
= 0
.304
8 m
)
Not
e 1:
Reg
ardl
ess
of it
s si
ze, a
ny A
SM
E ta
nk fi
lled
on s
ite m
ust b
e lo
cate
d so
that
the
fillin
g co
nnec
tion
and
fixed
liqu
id le
vel g
auge
are
at l
east
10
ft. a
way
from
any
ext
erna
lso
urce
of i
gniti
on (i
.e.,
open
flam
e, w
indo
w A
/C, c
ompr
esso
r, et
c.),
inta
ke to
dire
ct v
ente
dga
s ap
plia
nce
or in
take
to a
mec
hani
cal v
entil
atio
n sy
stem
.
Not
e 2:
Thi
s di
stan
ce m
ay b
e re
duce
d to
no
less
than
10
ft.(3
m) f
or a
sin
gle
cont
aine
r of 1
,200
-gal
(4.5
-m3) w
ater
capa
city
or l
ess
prov
ided
suc
h co
ntai
ner i
s at
leas
t 25
ft (7
.6m
) fro
m a
ny o
ther
LP
-Gas
con
tain
er o
f mor
e th
an 1
25-g
al(0
.5-m
3 ) w
ater
cap
acity
.
501-
2000
Gal
. w.c
.
14
Cen
tral
A/C
com
pres
sor (
sour
ce o
fig
nitio
n)
(1 ft
= =
0.30
48 m
)
Cra
wl s
pace
ope
ning
,w
indo
ws,
or e
xhau
st fa
n
10-ft
Min
. (N
ote
2)
Cra
wl s
pace
ope
ning
10-ft
Min
. (N
ote
2)
10-f
t Min
.(N
ote
1)10-ft
Min
. (N
ote
1)
Inta
ke to
dire
ct v
ent
appl
ianc
eW
indo
w a
ir co
nditi
oner
(sou
rce
of ig
nitio
n)
10-ft
Min
. (N
ote
1)
2000
Gal
. w.c
. or l
ess
Nea
rest
line
of a
djoi
ning
pro
pert
yth
at m
ay b
e bu
ilt u
pon
CONTAINER LOCATION (cont)
Rep
rint
ed fr
om N
FPA
58,
Fig
ure
I.1(c
), 2
002
ed.
Figure 5 Below Ground ASME Containers
Not
e 2:
No
part
of a
n un
derg
roun
d co
ntai
ner s
hall
bele
ss th
an 1
0 ft.
from
an
impo
rtan
t bui
ldin
g or
line
of
adjo
inin
g pr
oper
ty th
at m
ay b
e bu
ilt u
pon.
Not
e 1:
The
relie
f val
ve, f
illin
g co
nnec
tion,
and
liqu
id fi
xed
max
imum
leve
l gau
ge v
ent c
onne
ctio
n at
the
cont
aine
r mus
tbe
at l
east
10
ft. fr
om a
ny e
xter
ior s
ourc
e of
igni
tion,
open
ings
into
dire
ct-v
ent a
pplia
nces
, or m
echa
nica
lve
ntila
tion
air i
ntak
es.
15
CONTAINER PREPARATION FORREMOVAL OF WATER AND AIRCONTAMINANTSBoth water and air are contaminants that can seriouslyhinder the proper operation of the LP-Gas system and theconnected appliances if not effectively removed. The fol-lowing procedures will help increase system performanceand decrease the number of service calls.
REMOVING WATER FROM CONTAINERSWater in LP-Gas cylinders and tanks can contaminate thegas, causing regulator freezeups and erratic applianceperformance. Neutralize any moisture in the container byadding anhydrous methanol (99.85% pure) according tothe amount shown in the Table below.
This will minimize freezeup problems for normal amountsof water in a container. However, this water may still causecorrosion or sediment problems. Large amounts of watershould be drained from the tank.
Warning: Do not substitute other alcohols in place ofmethanol.
6elbaT
EZISRENIATNOCFOTNUOMAMUMINIMDERIUQERLONAHTEM
rednilyc.bl001knat.lag051knat.lag052knat.lag005knat.lag0001
)secnuodiulf2(tniP8/1tnip1trauq1strauq2nollag1
16
PURGING AIR FROM CONTAINERSAir in the LP-Gas can cause appliance pilot lights to beextinguished easily. It can also lead to excessive con-tainer pressure, making the safety relief valve open. Sincenearly all containers are shipped from the fabricator underair pressure, it is extremely important to get rid of the airbefore the container is put in service.
DOT Cylinders
First, open the cylinder or service valves for several min-utes to allow air to bleed to atmosphere. Then, pressurethe cylinder with LP-Gas vapor and again open the cylin-der or service valve (repeat this step at least two times).
ASME Storage Tanks
Depending on the type of valves in the tank, (see Figure 6on page 17), purge the container as follows:
1) Bleed the air to atmosphere by opening the multi-pur-pose valve or the service valve for several minutesuntil air pressure is exhausted. Close the valve.
2) If a pressure gauge has not been installed in the multi-purpose valve side outlet, install a 0-300 psig gauge(Fisher Type J506). On tanks with service valves, in-stall a POL x 1/4” FNPT pipe coupling and 0-300 psiggauge in the service valve outlet.
3) Attach the truck vapor equalizing hose to the multi-purpose valve’s vapor equalizing valve or the separatevapor-equalizing valve.
4) Slowly open the shutoff valve on the end of the hose sothat the truck excess flow check valve does not slamshut.
17
PURGING AIR FROM CONTAINERS (Cont.)ASME Storage Tanks (cont.)
(5) Closely watch the pressure, and when the gaugereaches 15 psig, close the shutoff valve.
(6) Open the vapor service valve on the multi-purpose valve(or the separate service valve, after removing the adap-tor). Allow all pressure to be exhausted before closingthe multi-purpose valve or the service valve.
(7) Repeat steps 4 through 6 at least three more times tomake certain air has been purged from the tank.
Note: Do not purge tanks in this way on the customer’sproperty. Purge them in a safe place at the bulk plant site.
VAPOREQUALIZING
VALVE
SHUTOFF VALVE
PRESSURE GAUGE
SHUTOFFVALVE
SERVICE VALVE
PIPECOUPLING
PRESSUREGAUGE
SERVICE VALVEOUTLET
TO TRUCK VAPOREQUALIZING VALVE
TO TRUCK VAPOREQUALIZING VALVE
PURGING METHOD WITH SEPARATE VALVES
PURGING METHOD WITH MULTI-PURPOSE VALVE
Figure 6
MULTI-PURPOSEVALVE
18
PIPE AND TUBING SIZINGThe proper selection of pipe and tubing sizes is essentialfor the efficient operation of the LP-Gas appliance. Gen-eral consideration must be given to the maximum gasdemand requirements of the system and the allowablepressure loss from the point of delivery to the inletconnection of the gas appliance.
Four different areas of sizing requirements must be ad-dressed:
1) Sizing between First-Stage and Second-StageRegulators
2) Sizing between Second-Stage Regulator and Appliance
3) Sizing between 2 PSI Service and Line Pressure Regulators
4) Sizing between Line Pressure Regulator and Appli-ance
The following directions and examples, as well as tables7-10 starting on page 23, will assist you in determiningthe proper selection of pipe and tubing sizing for thesedifferent areas. All data in the tables are calculated perNFPA Pamphlet Nos. 54 and 58.
19
PIPE AND TUBING SIZING (Cont.)Directions for Sizing between First-Stageand Second-Stage Regulators
(Based on NFPA 54 Hybrid Pressure Method)1) Measure the required length of pipe or tubing from the
outlet of the first-stage regulator to the inlet of the sec-ond-stage regulator.
2) Determine the maximum gas demand requirementsof the system by adding the BTU/HR inputs from thenameplates of all the appliances or by referring to Table3 on page 5.
3) Select the pipe or tubing required from Tables 7a, b,and c on pages 23-25.
Directions for Sizing Between Second-Stage Regulator and Appliance
(Based on NFPA 54 Longest Length Method)1) Measure the length of pipe or tubing from the outlet of
the second-stage regulator to the most remote appli-ance. (Note: This is the only length needed to size thesecond-stage system.)
2) For each outlet and section of pipe, determine the spe-cific gas demand requirements by adding the BTU/HR inputs from the nameplates of each appliance orby referring to Table 3 on page 5.
3) Select the pipe or tubing required for each section fromTable 8a or 8b on pages 26 and 27.
20
PIPE AND TUBING SIZING (Cont.)Determine the sizes of pipe or tubing required for this two-stageLP-Gas installation.
Example:A private home is to be supplied with a LP-Gas system serving acentral furnace, range and water heater. The gas demand andpiping lengths are shown on the sketch below.
Figure 7 Fisher 1stStage Regulator
Fisher 2nd StageRegulator
12’ 10’
10’ 30’15’Section 1 Section 2
CFURNACE
120,000 BTU/HR
BRANGE
75,000 BTU/HR
AWATERHEATER
40,000BTU/HR
25’
For First-Stage:1) Length of first-stage piping = 25 feet (round up to 30 ft. for use
in Table 7a, b, c.).2) Total gas demand = 40,000 + 75,000 + 120,000 = 235,000
BTU/HR.3) From Tables 7a, b, and c, use 1/2” iron pipe; or 1/4” Type L or
3/8” ACR copper tubing or 1/2” plastic tubing. (Assume a 10psig first-stage regulator setting and a 1 psig pressure drop.)
For Second-Stage:1) Total second-stage piping length = 30 + 10 + 15 = 55 feet
(round up to 60 ft. for use in Table 8a and 8b).2) Gas demand requirements and pipe selection from Table 8a
and 8b (Assume a 11” w.c. setting and 1/2” w.c. pressure drop):For Outlet A, demand = 40,000 BUT/HR, use 1/2” iron pipe or 3/8”
Type L or 5/8" ACR copper tubing.For Outlet B, demand = 75,000 BUT/HR, use 1/2” iron pipe or 1/2”
Type L or 5/8” ACR copper tubing.For Outlet C, demand = 120,000 BUT/HR, use 3/4” iron pipe or
5/8” Type L or 3/4” ACR copper tubing.For Section 1, demand = 40,000 + 75,000 = 115,000 BTU/HR, use
3/4” iron pipe or 5/8” Type L or 3/4” ACR copper tubing.For Section 2, demand = 40,000 + 75,000 + 120,000 = 235,000
BTU/HR, use 1” iron pipe.
21
PIPE AND TUBING SIZINGDirections for Sizing Between 2 PSI ServiceRegulator and Line Pressure Regulator1) Measure the length of CSST tubing from the outlet of the 2 PSI
service regulator to the inlet of the line pressure regulator.
2) Determine the maximum gas demand requirements of thesystem by adding the BTU/HR inputs from the nameplates ofall the appliances or by referring to Table 3 on page 5.
3) Use the correct footage column, or next higher column inTable 9. Select CSST tubing size when capacity in columnexceeds gas demand.
Directions for Sizing Between LinePressure Regulator and Appliance1) Measure the length of CSST tubing from the outlet of the line
pressure regulator to each of the appliances.
2) For each outlet and section of CSST tubing, determine thespecific gas demand requirements by adding the BTU/HRinputs from the nameplates of each appliance or by referringto Table 3 on page 5.
3) Use the correct footage column, or next higher column inTable 10. Select CSST tubing size when capacity in columnexceeds gas demand.
Example:
A typical single family home with four appliances is to be suppliedwith a LP-Gas system. The piping is arranged in parallel with adistribution manifold branching CSST runs to the appliances. Thesupply pressure (downstream of the service regulator) is 2 psigand the outlet pressure of the line pressure regulator is set to 11”w.c. (see next page).
22
PIPE AND TUBING SIZINGDetermine the sizes of pipe or tubing required for this in-house LP-Gas installation.
From 2 PSI Service Regulator to LineRegulator:
1) Length of section A tubing = 20 feet
2) Total gas demand = 80,000 + 36,000 + 28,000 +52,000 = 196,000 BTU/HR
3) From Table 9, use 25’ column. Select 3/8” CSST forrun A, as it has capacity over 196,000 BTU/HR(262,000). (Assume a 2 psig second-stage regulatorsetting and 1 psig pressure drop)
From Line Pressure Regulator to Each Appliance:
1) For line B, length= 10 feet; gas demand = 80,000 BTUFor line C, length= 10 feet; gas demand = 36,000 BTUFor line D, length= 30 feet; gas demand = 28,000 BTUFor line E, length= 35 feet; gas demand = 52,000 BTU
2) CSST Tubing selection from Table 10 (Assume a 11”w.c. setting and 0.5” w.c. pressure drop):
Figure 8
2 PSIService
RegulatorREGULATOR
MANIFOLD
xxxxx
A = 20ft
FURNACE80,000 BTU/
HR
B = 10ft C = 10ftWATER HEATER36,000 BTU/HR
DRYER28,000 BTU/HR
RANGE 52,000 BTU/HR
E = 35ft
D = 30ft
xxx
xxx
ENIL TFHTGNEL 0001DAOLRH/UTB
0001YTICAPACTSSCRH/UTB
TCELESEZISTSSC
BCDE
010103*53
08638225
921058246
2/18/38/32/1
01elbaTninmuloc'04esU*
R
23
PIPE AND TUBING SIZING (cont.)TA
BLE
7A
PIP
E SI
ZIN
G B
ETW
EEN
FIR
ST-S
TAG
E (H
IGH
PR
ESSU
RE
REG
ULA
TOR
) AN
D S
ECO
ND
-STA
GE
(LO
W P
RES
SUR
E R
EGU
LATO
R)
Max
imum
Und
ilute
d Pr
opan
e C
apac
ities
bas
ed o
n 10
psi
g fir
st s
tage
set
ting
and
1 ps
ig p
ress
ure
drop
. C
apac
ities
in 1
000
BTU
per
hou
rSc
hedu
le 4
0 Pi
pe S
ize,
inch
es (A
ctua
l Ins
ide
Dia
met
er, i
nche
s)Pi
ping
Len
gth,
Feet
1/2
NPT
(0.6
22")
3/4
NPT
(0.8
24")
1 N
PT(1
.049
")1
1/4
NPT
(1.3
8")
1 1/
2 N
PT(1
.61"
)2
NPT
(2.0
67")
3 N
PT(3
.068
")3
1/2
NPT
(3.5
48")
4 N
PT(4
.026
")30 40 50 60 70 80 90 10
015
020
025
030
035
040
045
050
060
070
080
090
010
0015
0020
00
1,83
41,
570
1,39
11,
261
1,16
01,
079
1,01
295
676
865
758
252
848
645
242
440
036
333
431
029
127
522
118
9
3,83
53,
283
2,90
92,
636
2,42
52,
256
2,11
72,
000
1,60
61,
374
1,21
81,
104
1,01
594
588
683
775
969
864
960
957
546
239
5
7,22
56,
184
5,48
04,
966
4,56
84,
250
3,98
83,
767
3,02
52,
589
2,29
42,
079
1,91
31,
779
1,66
91,
577
1,42
91,
314
1,22
31,
147
1,08
487
074
5
14,8
3412
,696
11,2
5210
,195
9,37
98,
726
8,18
77,
733
6,21
05,
315
4,71
14,
268
3,92
73,
653
3,42
83,
238
2,93
42,
699
2,51
12,
356
2,22
51,
787
1,52
9
22,2
2519
,022
16,8
5915
,275
14,0
5313
,074
12,2
6711
,587
9,30
57,
964
7,05
86,
395
5,88
35,
473
5,13
54,
851
4,39
54,
044
3,76
23,
530
3,33
42,
677
2,29
1
42,8
0436
,634
32,4
6829
,419
27,0
6525
,179
23,6
2422
,315
17,9
2015
,337
13,5
9312
,316
11,3
3110
,541
9,89
09,
342
8,46
57,
788
7,24
56,
798
6,42
15,
156
4,41
3
120,
604
103,
222
91,4
8482
,891
76,2
5870
,944
66,5
6462
,876
50,4
9243
,214
38,3
0034
,703
31,9
2629
,701
27,8
6726
,323
23,8
5121
,943
20,4
1319
,153
18,0
9214
,528
12,4
35
176,
583
151,
132
133,
946
121,
364
111,
654
103,
872
97,4
6092
,060
73,9
2763
,272
56,0
7750
,810
46,7
4443
,487
40,8
0238
,541
34,9
2132
,127
29,8
8828
,043
26,4
8921
,272
18,2
06
245,
995
210,
539
186,
597
169,
071
155,
543
144,
703
135,
770
128,
247
102,
987
88,1
4478
,120
70,7
8265
,119
60,5
8156
,841
53,6
9148
,648
44,7
5641
,637
39,0
6636
,902
29,6
3325
,362
Dat
a ta
ken
and
repr
inte
d fr
om T
able
12.
22 i
n N
FPA
54,
2002
ed.
24
PIPE AND TUBING SIZING (cont.)
Table 7b Pipe Sizing Between First-Stageand Second-Stage Regulators
Minimum undiluted propane capacities listed are based on a 10 psig first stagesetting and 1 psig pressure drop. Capacities in 1,000 BTU/HR.
Type ACR (REFRIGERATION) Type L Tubing
Nominal 3/8" 1/2" 5/8" 3/4" 7/8" 1/4" 3/8" 1/2" 5/8" 3/4"
Outside (0.375) (0.500) (0.625) (0.750) (0.875) (0.375) (0.500) (0.625) (0.750) (0.875)
Inside 0.311 0.436 0.555 0.68 0.785 0.315 0.430 0.545 0.666 0.785
Length(Ft.)
30 299 726 1367 2329 3394 309 700 1303 2205 3394
40 256 621 1170 1993 2904 265 599 1115 1887 2904
50 227 551 1037 1766 2574 235 531 988 1672 2574
60 206 499 939 1600 2332 213 481 896 1515 2332
70 189 459 864 1472 2146 196 443 824 1394 2146
80 176 427 804 1370 1996 182 412 767 1297 1996
90 165 401 754 1285 1873 171 386 719 1217 1873
100 156 378 713 1214 1769 161 365 679 1149 1769
150 125 304 572 975 1421 130 293 546 923 1421
200 107 260 490 834 1216 111 251 467 790 1216
250 95 230 434 739 1078 90 222 414 700 1078
300 86 209 393 670 976 89 201 375 634 976
350 79 192 362 616 898 82 185 345 584 898
400 74 179 337 573 836 76 172 321 543 836
450 69 168 316 538 784 71 162 301 509 784
500 65 158 298 508 741 68 153 284 481 741
600 59 144 270 460 671 61 138 258 436 671
700 54 132 249 424 617 56 127 237 401 617
800 51 123 231 394 574 52 118 221 373 574
900 48 115 217 370 539 49 111 207 350 539
1000 45 109 205 349 509 46 105 195 331 509
1500 36 87 165 281 409 37 84 157 266 409
2000 31 75 141 240 350 32 72 134 227 350
Table Reprinted From NFPA Pamphlet 54-1996.
25
PIPE AND TUBING SIZING (cont.)
Tabl
e R
eprin
ted
from
Tabl
e 12
.15
and
12.1
6 fro
m N
FPA
58, 2
001
editio
n.
TAB
LE 7
C P
OLY
ETH
YLEN
E P
LAST
IC T
UB
E A
ND
PIP
E S
IZIN
G B
ETW
EEN
FIR
ST-
STA
GE
AN
D S
ECO
ND
-STA
GE
REG
ULA
TOR
SM
axim
um u
ndilu
ted
prop
ane
capa
citie
s lis
ted
are
base
d on
10
psig
firs
t sta
ge s
ettin
g an
d 1
psi p
ress
ure
drop
. Cap
aciti
es in
100
0 B
TU/H
R
Leng
th o
fP
ipe
orTu
bing
, Fee
t
Pla
stic
Tub
ing
Size
(CTS
) and
Pip
e S
ize
(IPS)
(Dim
ensi
ons
in P
aren
thes
is a
re In
side
Dia
met
er)
1/2
in. C
TS S
DR
7.00
(0.4
45)
1 in
. CTS
SD
R11
.00
(0.9
27)
1/2
in. I
PS
SD
R9.
33 (0
.660
)3/
4 in
. IP
S S
DR
11.0
(0.8
60)
1 in
. IPS
SD
R11
.00
(1.0
77)
1-1/
4 in
. IP
S S
DR
10.0
0 (1
.328
)2
in. I
PS
SD
R 1
1.00
(1.9
43)
30 40 50 60 70 80 90 100
125
150
175
200
225
250
275
300
350
400
450
500
600
700
800
900
1000
1500
2000
762
653
578
524
482
448
421
397
352
319
294
273
256
242
230
219
202
188
176
166
151
139
129
121
114
92 79
5225
4472
3964
3591
3304
3074
2884
2724
2414
2188
2013
1872
1757
1659
1576
1503
1383
1287
1207
1140
1033
951
884
830
784
629
539
2143
1835
1626
1473
1355
1261
1183
1117
990
897
826
778
721
681
646
617
567
528
495
468
424
390
363
340
322
258
221
4292
3673
3256
2950
2714
2525
2369
2238
1983
1797
1653
1539
1443
1363
1294
1235
1136
1057
992
937
849
781
726
682
644
517
443
7744
6628
5874
5322
4896
4555
4274
4037
3578
3242
2983
2775
2603
2459
2336
2228
2050
1907
1789
1690
1531
1409
1311
1230
1162
933
798
1341
611
482
1017
692
2084
8378
9174
0469
9461
9956
1651
6748
0745
1042
6040
4638
6035
5133
0431
0029
2826
5324
4122
7121
3120
1216
1613
83
3640
231
155
2761
225
019
2301
721
413
2009
118
978
1682
015
240
1402
013
043
1223
811
560
1097
910
474
9636
8965
8411
7945
7199
6623
6761
5781
5461
4385
3753
26
PIPE AND TUBING SIZING (cont.)
Dat
a ta
ken
and
repr
inte
d fro
m Ta
ble
12.2
4 in
NFP
A 54
, 200
2 ed
.
TAB
LE 8
A P
IPE
SIZI
NG
BET
WEE
N S
ECO
ND
-STA
GE
(LO
W P
RES
SUR
E R
EGU
LATO
R) A
ND
APP
LIAN
CE
Max
imum
Und
ilute
d Pr
opan
e C
apac
ities
bas
ed o
n 11
inch
w.c
. set
ting
and
0.5
inch
w.c
. pre
ssur
e dr
op.
Cap
aciti
es in
100
0 B
TU p
er h
our
Sche
dule
40
Pipe
Siz
e, in
ches
(Act
ual I
nsid
e D
iam
eter
, inc
hes)
Pipi
ng L
engt
h,Fe
et1/
2 N
PT(0
.622
")3/
4 N
PT(0
.824
")1
NPT
(1.0
49")
1 1/
4 N
PT(1
.38"
)1
1/2
NPT
(1.6
1")
2 N
PT(2
.067
")3
NPT
(3.0
68")
3 1/
2 N
PT(3
.548
")4
NPT
(4.0
26")
1029
160
81,
450
2,35
23,
523
6,78
619
,119
27,9
9338
,997
2020
041
878
71,
616
2,42
24,
664
13,1
4119
,240
26,8
0230
160
336
632
1,29
81,
945
3,74
510
,552
15,4
5021
,523
4013
728
754
11,
111
1,66
43,
205
9,03
113
,223
18,4
2150
122
255
480
984
1,47
52,
841
8,00
411
,720
16,3
2660
110
231
434
892
1,33
72,
574
7,25
310
,619
14,7
9380
9419
737
276
31,
144
2,20
36,
207
9,08
812
,661
100
8417
533
067
71,
014
1,95
25,
501
8,05
511
,221
125
7415
529
260
089
91,
730
4,87
67,
139
9,94
515
067
140
265
543
814
1,56
84,
418
6,46
89,
011
200
5812
022
746
569
71,
342
3,78
15,
536
7,71
225
051
107
201
412
618
1,18
93,
351
4,90
66,
835
300
4697
182
373
560
1,07
83,
036
4,44
66,
193
350
4289
167
344
515
991
2,79
34,
090
5,69
840
040
8315
632
047
992
22,
599
3,80
55,
301
27
Dat
a ca
lcul
ated
from
For
mul
a fro
m N
FPA
54, 2
002
ed.
EC
NAILPPAD
NAE
GATSD
NO
CESNEE
WTEB
GNIZIS
EB
UTB8
ELBAT
.porderusserp
nmulocreta
whcni
5.0dna
gnittesn
mulocretaw
hcni11
nodesab
eraseticapac
enaporpdetulidnu
mumixa
M.ruo
HrepUT
B0001
niera
seiticapaC
epyT)noitaregirfe
R(R
CAgnibuT
LepyT
lami
moN
8/32/1
8/54/3
8/74/1
8/32/1
8/54/3
edistuO
573.0005.0
526.0057.0
578.0573.0
005.0526.0
057.0578.0
edisnI113.0
634.0555.0
86.0587.0
513.0034.0
545.0666.0
587.0,htgneL
teeF01 02 03 04 05 06 08001521051002052003053004
74 23 62 22 02 81 51 41 21 11 9 8 7 7 6
51197 36 45 84 34 73 33 92 62 32 02 81 71 61
612841911201
09 28 07 26 55 05 34 83 43 23 92
763352302471451931911601
49 58 37 46 85 45 05
535863692352422302471451731421601
49 58 87 37
94 43 72 32 02 91 61 41 21 11 01 9 8 7 7
01167 16 25 64 24 63 23 82 62 22 91 81 61 51
602141311
79 68 87 76 95 25 84 14 63 33 03 82
843932291461641231311001
98 08 96 16 55 15 74
535863692352422302471451731421601
49 58 87 37
28
PIPE AND TUBING SIZING (cont.)Ta
ble
9 M
axim
um C
apac
ity o
f CSS
T*
CSST
TUBE
SIZE
EHD*
* FLO
WDE
SIGN
ATIO
N
In Th
ousa
nds o
f BTU
per
Hou
r of U
ndilu
ted
Prop
ane
at a
pre
ssur
e of
2.0
psi
and
a pr
essu
re d
rop
of1.
0 ps
i (Ba
sed
on a
1.5
0 sp
ecific
gra
vity g
as.)
TUBI
NG L
ENGT
H (F
EET)
1025
3040
5075
8010
015
020
025
030
040
050
03/
8 Inc
h---
1/2
Inch
---3/
4 Inc
h--- --- 1Inc
h1
1/4
Inch
1 1/
2 Inc
h2
Inch
13 15 18 19 23 25 30 31 37 46 62
426
558
927
1,10
61,
735
2,16
84,
097
4,72
07,
128
15,1
7434
,203
262
347
591
701
1,12
01,
384
2,56
02,
954
4,56
49,
549
21,6
80
238
316
540
640
1,02
71,
266
2,33
12,
692
4,17
68,
708
19,8
01
203
271
469
554
896
1,10
02,
012
2,32
33,
631
7,52
917
,159
181
243
420
496
806
986
1,79
42,
072
3,25
86,
726
15,3
57
147
196
344
406
663
809
1,45
71,
685
2,67
55,
480
12,5
51
140
189
333
393
643
768
1,41
01,
629
2,59
15,
303
12,1
54
124
169
298
350
578
703
1,25
61,
454
2,32
54,
738
10,8
77
101
137
245
287
477
575
1,02
11,
182
1,90
83,
860
8,89
0
86 118
213
248
415
501
880
1,01
91,
658
3,33
77,
705
77 105
191
222
373
448
785
910
1,48
72,
981
6,89
5
69 96 173
203
343
411
716
829
1,36
32,
719
6,29
6
60 82 151
175
298
355
616
716
1,16
32,
351
5,45
7
53 72 135
158
268
319
550
638
1,02
72,
101
4,88
3Ta
ble
does
not
incl
ude
effe
ct o
f pre
ssur
e dr
op a
cros
s the
line
regu
lato
r. W
here
regu
lato
r los
s exc
eeds
1/2
psi
(bas
ed o
n 13
inch
w.c
. out
let p
ress
ure)
, do
not u
se th
is ta
ble.
Con
sult w
ith re
gula
tor m
anuf
actu
rer f
or p
ress
ure
drop
s an
d ca
paci
ty fa
ctor
s. P
ress
ure
drop
s ac
ross
a re
gula
tor m
ay v
ary
with
flow
rate
. CAU
TIO
N: C
apac
ities
show
n in
tabl
e m
ay e
xcee
d m
axim
um ca
paci
ty fo
r a se
lect
ed re
gula
tor.
Con
sult w
ith re
gula
tor o
r tub
ing
man
ufac
ture
r for
qui
danc
e.* T
able
incl
udes
loss
es fo
r fou
r 90-
degr
ee b
ends
and
two
end
fittin
gs. T
ubin
g ru
ns w
ith la
rger
num
bers
of b
end
and/
or fit
tings
sha
ll be
incr
ease
d by
an
equi
vale
nt le
ngth
of t
ubin
g to
the
follo
win
equ
atio
n: L
= 1
.3n
whe
reL
is th
e ad
ditio
nal le
ngth
(ft)
of tu
bing
and
N is
the
num
ber o
f add
ition
al fi
tting
s an
/or b
ends
.**
EDH
- Eq
uiva
lent
hyd
raul
ic D
iam
eter
- A
mea
sure
of t
he re
lativ
e hy
drau
lic e
ffici
ency
bet
wee
n di
ffere
nt tu
bing
siz
es. T
he g
reat
er th
e va
lue
of E
HD
, the
gre
ater
the
gas
capa
city
of t
he tu
bing
.D
ata
take
n an
d re
prin
ted
from
Tab
le 1
2.29
in N
FPA
54, 2
002
ed.
29
PIPE AND TUBING SIZING (cont.)Ta
ble
9A P
ipe
Sizi
ng B
etw
een
2 PS
I Reg
ulat
or a
nd A
pplia
nce
Reg
ulat
orM
axim
um U
ndilu
ted
Prop
ane
Cap
aciti
es b
ased
on
2 ps
i set
ting
and
1 ps
i pre
ssur
e dr
op.
Cap
aciti
es in
100
0 B
TU p
er h
our
Sche
dule
40
Pipe
Siz
e, in
ches
(Act
ual I
nsid
e D
iam
eter
, inc
hes)
Pipi
ngLe
ngth
, Fee
t1/
2 N
PT(0
.622
")3/
4 N
PT(0
.824
")1
NPT
(1.0
49")
1 1/
4 N
PT(1
.38"
)1
1/2
NPT
(1.6
1")
2 N
PT (2
.067
")2
1/2
NPT
(2.4
69")
3 NP
T(3
.068
")4
NPT
(4.0
26")
102,
676
5,59
510
,539
21,6
3832
,420
62,4
3899
,516
175,
927
358,
835
201,
839
3,84
57,
243
14,8
7222
,282
42,9
1368
,397
120,
914
246,
625
301,
477
3,08
85,
817
11,9
4217
,893
34,4
6154
,925
97,0
9819
8,04
9
401,
264
2,64
34,
978
10,2
2115
,314
29,4
9447
,009
83,1
0316
9,50
4
501,
120
2,34
24,
412
9,05
913
,573
26,1
4041
,663
73,6
5315
0,22
9
601,
015
2,12
23,
998
8,20
812
,298
23,6
8537
,750
66,7
3513
6,11
8
7093
41,
952
3,67
87,
551
11,3
1421
,790
34,7
2961
,395
125,
227
8086
91,
816
3,42
27,
025
10,5
2620
,271
32,3
0957
,116
116,
499
9081
51,
704
3,21
06,
591
9,87
619
,020
30,3
1453
,590
109,
307
100
770
1,61
03,
033
6,22
69,
329
17,9
6628
,635
50,6
2110
3,25
1
125
682
1,42
72,
688
5,51
88,
268
15,9
2325
,378
44,8
6591
,510
150
618
1,29
32,
435
5,00
07,
491
14,4
2722
,995
40,6
5182
,914
175
569
1,18
92,
240
4,60
06,
892
13,2
7321
,155
37,3
9876
,280
200
529
1,10
62,
084
4,27
96,
411
12,3
4819
,681
34,7
9270
,964
Dat
a ta
ken
and
repr
inte
d fro
m Ta
ble
12.2
3 in
NFP
A 54
, 200
2 ed
.
30
Dat
a ca
lcul
ated
from
For
mul
a in
NFP
A 54
, 200
2 ed
.
Tabl
e 9B
Tub
e S
izin
g B
etw
een
Seco
nd S
tage
and
App
lianc
e
Max
imum
und
ilute
d pr
opan
e ca
paci
tes
are
base
d on
2 p
si s
ettin
g an
d 1
psi p
ress
ure
drop
. C
apac
ities
are
in 1
000
BTU
per
Hou
r.
Type
ACR
(Ref
riger
atio
n)Ty
pe L
Tub
ing
Nom
imal
3/8
1/2
5/8
3/4
7/8
1/4
3/8
1/2
5/8
3/4
Out
side
0.37
50.
500
0.62
50.
750
0.87
50.
375
0.50
00.
625
0.75
00.
875
Insi
de0.
311
0.43
60.
555
0.68
0.78
50.
315
0.43
00.
545
0.66
60.
785
Leng
th, F
eet
10 20 30 40 50 60 80 100
125
150
200
250
300
350
400
434
298
239
205
182
165
141
125
111
100
86 76 69 63 59
1053
723
581
497
441
399
342
303
268
243
208
184
167
154
143
1982
1362
1094
936
830
752
644
570
506
458
392
347
315
290
269
3377
2321
1864
1595
1414
1281
1096
972
861
780
668
592
536
493
457
4922
3383
2716
2325
2061
1867
1598
1416
1255
1137
973
863
782
719
669
449
308
248
212
188
170
146
129
114
104
89 79 71 66 61
1015
698
560
479
425
385
330
292
259
235
201
178
161
148
138
1890
1299
1043
893
791
717
614
544
482
437
374
331
300
276
257
3198
2198
1765
1511
1339
1213
1038
920
816
739
632
560
508
467
435
4922
3383
2716
2325
2061
1867
1598
1416
1255
1137
973
863
782
719
669
31
* Tab
le in
clud
es lo
sses
for f
our 9
0-de
gree
ben
ds a
nd tw
o en
d fit
tings
. Tub
ing
runs
with
larg
er n
umbe
rs o
f ben
d an
d/or
fittin
gs s
hall b
e in
crea
sed
by a
n eq
uiva
lent
leng
thof
tubi
ng to
the
follo
win
equ
atio
n: L
= 1
.3n
whe
re L
is th
e ad
ditio
nal le
ngth
(ft)
of tu
bing
and
N is
the
num
ber o
f add
ition
al fi
tting
s an
/or b
ends
.**
EDH
- Eq
uiva
lent
hyd
raul
ic D
iam
eter
- A
mea
sure
of t
he re
lativ
e hy
drau
lic e
ffici
ency
bet
wee
n di
ffere
nt tu
bing
siz
es. T
he g
reat
er th
e va
lue
of E
HD
, the
gre
ater
the
gas
capa
city
of th
e tu
bing
.D
ata
take
n an
d re
prin
ted
from
Tab
le 1
2.28
in N
FPA
54, 2
002
ed.
Tabl
e 10
Max
imum
Cap
acity
of C
SST
*
CS
STTU
BE
SIZ
E
EH
D**
FLO
WD
ESI
GN
ATIO
N
In T
hous
ands
of B
TU p
er H
our o
f Und
ilute
d P
ropa
ne a
t a p
ress
ure
of 1
1 in
. W.C
. and
a p
ress
ure
drop
of
0.5-
in. w
.c. (
Bas
ed o
n a
1.50
spe
cific
gra
vity
gas
.)
TUB
ING
LE
NG
TH (F
EET
)5
1015
2025
3040
5060
7080
9010
015
020
025
030
03/
8 In
ch---
1/2
Inch
---3/
4 In
ch--- ---
1 In
ch1
1/4
Inch
1 1/
2 In
ch2
Inch
13 15 18 19 23 25 30 31 37 46 62
72 99 181
211
355
426
744
863
1,41
52,
830
6,54
7
50 69 129
150
254
303
521
605
971
1,99
34,
638
39 55 104
121
208
248
422
490
775
1,62
33,
791
34 49 91 106
183
216
365
425
661
1,40
43,
285
30 42 82 94 164
192
325
379
583
1,25
42,
940
28 39 74 87 151
177
297
344
528
1,14
32,
684
23 33 64 74 131
153
256
297
449
988
2,32
7
20 30 58 66 118
137
227
265
397
884
2,08
2
19 26 53 60 107
126
207
241
359
805
1,90
2
17 25 49 57 99 117
191
222
330
745
1,76
1
15 23 45 52 94 109
178
208
307
656
1,55
4
15 22 44 50 90 102
169
197
286
656
1,55
4
14 20 41 47 85 98 159
186
270
621
1,47
5
11 15 31 36 66 75 123
143
217
506
1,20
5
9 14 28 33 60 69 112
129
183
438
1,04
5
8 12 25 30 53 61 99 117
163
390
934
8 11 23 26 50 57 90 107
147
357
854
SELECTING THE REGULATORRegulator performance curves show the capacity of aregulator at different inlet pressures, given the factorysetting for outlet pressure.
Figure 9 on page 33 shows a performance curve for aFisher Second-Stage Regulator. Gas flow rate is plottedhorizontally and regulator outlet pressure vertically. Thecurved line represents an inlet pressure of 10 psig. Forthe appliance to operate efficiently, the regulator outletpressure must not fall below 9” w.c.
Fisher rates this particular regulator at the point the 10psig inlet curve crosses the 9” w.c. horizontal line. Thus,the Fisher literature would rate this regulator at 1,375,000BTU/HR or more if the inlet pressure stays above 10 psig.
What you must know to select a regulator:
1. Appliance Load
2. Pipe Size
3. Inlet Pressure
4. Outlet Pressure
5. Gas Used (Propane/Butane)
6. Select From Manufacturer Catalog
32
OUTLET PRESSUREINCHES OF WATER COLUMN
CU
FT
/HR
BT
U/H
R
PR
OPA
NE
FL
OW
RA
TE
100
250,
000
200
500,
000
9101113 12
300
750,
000
400
1,00
0,00
050
01,
250,
000
600
1,50
0,00
0
10 P
SIG
Fig
ure
9
TYPICAL CAPACITY CURVE
33
34
REGULATOR SELECTION
1 Based on 30 psig inlet pressure and 20% droop2 Based on 10 psig inlet pressure and 20% droop3 Based on inlet pressure 20 psig greater than outlet pressure with 20% droop.
NOTE: The capacity BTU/HR column should be used forreference purposes only. The capacity will vary dependingon the pipe size, orifice size and outlet pressure setting.
TABLE 11
TYPE OFREGULATOR OR
SERVICECAPACITY, BTU/HR
RECOMMENDEDFISHER
REGULATORFirst-Stage1
(Reducestank pressure to10 psig or less)
1,100,0002,400,000
R122HR622H
Second-Stage2
(Reduces first stageoutlet pressure to14" w.c. or less)
875,000 - 1,375,0002,300,000 - 2,600,000
5,500,00010,500,000 - 14,500,000
R622HSRLS302GS202G
Integral Two-Stage1
(Combines a highpressure and a 2nd
stage regulator)
350,000750,000
R232R632
High Pressure3
(Reduces tankpressure to a lowerpressure in excess
of 1 psig)
750,000 -1,200,0002,625,000 - 5,250,000
13,000,000 - 38,000,0006,000,000 - 10,775,000
14,000,00029,295,000 -36,225,000
67C64 or 64SR
299H627
630-104/7899
2-PSI2 Service(Reduces 1st stagepressure to 2 psig)
1,400,0001,500,000
R652ER622E
35
TWO-STAGE REGULATIONAdvantages of Two-Stage RegulationUniform Appliance Pressure - Two-staging lets the first-stage regulator supply a nearly constant inlet pressure tothe second-stage regulator at the house. This means thesecond-stage regulator has an easier time of maintainingappliance pressure at 11” w.c., thus improving the systemefficiency.
Lower Installation Costs - Smaller pipe or tubing can beused between the first and second-stage regulators dueto the higher pressure, thus reducing installation andpiping material costs.
Freezeups - Two-stage systems reduce problems due toregulator freezeups caused by excessive water in gas.Larger orifices make it more difficult for ice to form andblock the passage area. The expansion of gas at twodifferent orifices in a two-stage system greatly reducesthe “refrigeration effect” that causes freezeups. See FisherBulletins LP-18 and LP-24 for more detailed informationon freezing regulators.
Flexibility of Installation - A high pressure regulator canfeed a number of low pressure regulators, thus enablingthe addition of appliances in the future to the same pres-sure line without affecting their individual performance.
Fewer Trouble Calls - With two-stage regulation, you canexpect fewer trouble calls due to pilot outage or burneradjustment. This means higher appliance efficiency, lowerservice costs and better customer relations.
36
REGULATOR INSTALLATION
A two-stage regulator system or an integral two-stageregulator shall be required on all fixed piping systemsthat serve appliance systems at 11” w.c. This includesR.V., manufactured housing and food service installations.(Exceptions: Small portable appliances and outdoorcooking appliances with input ratings of 100,000 BTU/HRor less, certain gas distribution systems utilizing multiplesecond-stage regulators and systems that provide anequivalent level of overpressure protection).
This standard along with changes in UL 144 requiringincreased regulator relief valve capacity or an overprotec-tion shutoff device, results in the maximum pressure down-stream of the second-stage regulator being limited to 2psig even with a regulator seat failure.
See Fisher Bulletin LP-15 for more detailed informationon regulator operation, installation and maintenance.
TWO-STAGE REGULATIONTwo Regulators, one at tank and one at building,
reduce pressure down to burner pressure (11” w.c.)
Figure 10
FIRST–STAGE REGULATOR
USUALLY 10 PSIG
SECOND–STAGE REGULATOR
11” WC
37
REGULATOR INSTALLATIONRegulator VentsRegulators should be installed in accordance with NFPA58 and any other applicable regulations, as well as themanufacturer’s instructions. The following guidelinesshall be followed:
Outdoor Installations - A regulator installed outdoors with-out a protective hood must have its vent pointed verticallydown, as shown in the drawing.
The regulator should be at least 18 inches above ground.Do not install the regulator where there can be excessivewater accumulation or ice formation, such as directly be-neath a downspout, gutter or roofline. All vent openingsmust be at least three horizontal feet from any buildingopening and no less than five feet in any direction fromany source of ignition, openings into direct vent appliancesor mechanical ventilation intakes.
Horizontally mounted regulators, such as on single cylin-der installations, must be installed underneath aprotective cover. On ASME tank installations with theregulator installed under the tank dome, the regulator ventshould slope slightly down enough to allow anycondensation to drain from the spring case. The regulatorvent should be positioned far enough back from the tankdome slot so that it is protected from the weather. Thehood should be kept closed.
Regulators without “drip lip” vents must be installed undera protective cover.
VENT POINTEDDOWN
Figure 11
38
REGULATOR INSTALLATIONRegulator Vents (cont.)Indoor Installations - In a fixed pipe system, regulators in-stalled indoors require a vent line to the outside air. Ascreened vent assembly (Fisher Type Y602 series or equiva-lent) must be used at the end of the vent line. The ventassembly position and location precautions are the sameas for regulator vents. The vent line must be the same sizeas the regulator vent and adequately supported. See Fig-ure below.
Underground Tanks - A vent tube is required on these in-stallations to prevent water from entering the regulator’sspring case. The vent tube connects to the regulator ventand terminates above any possible water level, see Figurebelow. Be sure that the ground slopes away from the tankdome as illustrated. See Figure below.
Moderately crown surfacearound dome. This preventswater collecting and runninginto dome or standingaround dome.
End of regulator venttube located at topinside dome cover.
Water mark in domeat level above vent or
end of vent tuberequires replacement
of regulatorand correcting
installation.
Regulatorbonnet
closure capmust be tight.
FROMFIRST-STAGEREGULATOR
TOAPPLIANCE
VENT ASSEMBLY
DISCHARGEOPENING MUSTBE AT LEAST 3FT FROM ANYOPENINGBELOW IT
VENTLINE
BASEMENT
Figure 12
Figure 13
2” Minimum
39
LEAK TESTING METHODSThere are two primary methods for testing leaks in installa-tions:
Low Pressure Method
1) Inspect all connections and appliance valves to be surethey are tight or closed. This includes pilot valves.
2) Connect a low pressure gauge (Fisher Type 50P-2 orequivalent) to the burner orifice and open the valve.
3) Open the service valve at the tank to pressure the sys-tem. Close the service valve tightly.
4) The low pressure gauge should read at least 11” w.c.Slowly bleed off pressure by opening burner valve onthe appliance to vent enough gas to reduce the pres-sure to exactly 9” w.c.
5) If the pressure remains at 9” w.c. for 3 minutes, you canassume the system is leak tight. If the pressure drops,refer to the leak detection procedures on the next page.
6) After the leak is repaired, repeat steps 3, 4, and 5.
High Pressure Method
1) Inspect all connections and appliance valves to be surethey are tight or closed. This includes pilot valves.
2) Connect a test block . (Fisher Type J600 or equivalentin the service valve outlet at the tank, between thevalve’s outlet and the first regulator in the system.)
40
LEAK TESTING METHODSHigh Pressure Method (cont.)
3) Open the service valve at the tank to pressure the sys-tem. Close the service valve tightly.
4) Open an appliance valve until the test block’s pressuregauge drops to 10 psig.
5) The system should stand for 3 minutes without an in-crease or decrease in the 10-psig reading. If pressuredrops, refer to the leak detection procedure section. Ifpressure increases, then the service valve is leaking.
6) After any leaks are repaired, repeat steps 2, 3 and 4.
Leak Detection and Correction Procedures
1) Use a bubble leak detection solution, or mechanicalleak detector, (never a match or an open flame) whenchecking for leaks.
2) Apply the solution over every pipe or tubing joint andobserve carefully to see if the bubbles expand, indicat-ing a leak is present. A large leak can blow the solutionaway before bubbles have a chance to form.
3) To correct a leak on flaring tubing, first try to tighten theconnection. If this doesn’t work, reflare.
4) On threaded piping, try tightening or redoping first. Ifthe leak continues, take the connection apart and in-spect the threads. Cut new threads if necessary.
5) If steps 3 and 4 fail to correct the problem, look forsandholes in the pipe or fittings and check for splits inthe tubing. Replace whatever material is defective.
Note: Leaks caused by equipment such as gas cocks,appliances, valves, etc., will require repair of the faultypart or replacement of the entire device.
41
REGULATOR INSPECTIONThe following items should be checked at each gas deliv-ery and at regularly scheduled testing and maintenanceprogram intervals.
The customer should be instructed to turn off the tank ser-vice valve if gas can be smelled, pilot lights fail to stay on,or any other abnormal situation takes place.
Improper Installation
The regulator ventmust be pointeddown or under aprotective cover.Regulators without“drip lip” vents mustbe under a protec-tive cover. Properinstallation alsominimizes weatherrelated vent blockage and internal corrosion.
Vent Blockage
Make sure the regulator vent, vent assembly, or vent tubeis not blocked with mud, insect nests, ice, snow, paint, etc.The screen should be clean and properly installed.
Internal & External Corrosion
Replace any regulator that has had water in the spring caseor shows evidence of external or internal corrosion. Regu-lators that have been flooded or that have been installedhorizontally which minimizes moisture drainage, or on un-derground tanks, or in coastal areas are more susceptibleto internal corrosion.
To inspect for internal corrosion:
1) Remove the regulator’s closing cap and look down intothe spring case (a flashlight may be needed).
2) On some regulators it may be necessary to shut downthe system and remove the adjusting screw and mainspring to adequately see any internal corrosion.
Drip Lip
Figure 14
42
REGULATOR INSPECTION (cont.)Internal & External Corrosion (cont.)
3) Look for visible corrosion or water marks on the reliefvalve area and chimney (shaded area in the picturebelow).
4) Replace the regulator if corrosion is present.
Regulator Age
Locate and replace old regulators. Replace regulatorsthat are over 15 years of age or that have experiencedconditions (corrosion, underground systems, flooding, etc.)that would shorten their service life. Older regulators aremore likely to fail because of worn or corroded parts. Re-place with a two-stage regulator system.
Abnormal Pressure
Regulator disc wear (especially on older regulators) orforeign material (dirt, pipe scale, etc.) lodged between theregulator disc and orifice can cause higher than normaloutlet pressure to the appliances at lock up or extremelylow flows. A pressure test of the system will be required toverify the outlet pressure under these conditions. Replacethe regulator if pressure is high. Check the system for for-eign material and clean out or replace pigtails as needed.
Always retest the system after replacing a regulator.
See Fisher Bulletin LP-32 and the instruction manual formore detailed information on inspecting LP-Gas regula-tors.
Shaded area indicatesspot to examine forinternal corrosion.
Figure 15
43
TROUBLESHOOTING DOMESTICTANK FITTINGSA periodic inspection and maintenance program is rec-ommended for domestic tank fittings. The following brieflydiscusses ways to avoid and correct potential safety prob-lems with the most common domestic fittings.A more complete examination of this subject can be foundin NPGA Safety Bulletin 306.Filler ValvesAlways use a filling hose adaptor on the end of the hoseend valve during the filling process. After filling the tank,do not disconnect the Acme coupling from the filler valveuntil the Fill valve is closed and all pressure between thehose end valve and the Fill valve has been bled off. Ifpressure discharge continues, the filler valve may havemalfunctioned. DO NOT REMOVE THE FILL HOSE ASTHE INTERNAL PARTS MAY BE BLOWN OUT. If lighttapping does not close the Fill valve, disconnect the FillingHose Adaptor from the Hose End Valve, leaving the FillingHose Adaptor on the Fill valve. The tank will probablyhave to be emptied to replace the Fill valve.Some Fill valve designs allow the seat disc to be replacedwhile the tank is pressurized. On these designs, makesure the lower back check is still functioning by forcing openthe upper back check with an adaptor. Take care to dis-lodge only the upper back check and not both back checks.If there is little leakage with the upper back check open,then the lower back check is in place and the disc can bereplaced by following the manufacturer’s instructions.Relief ValvesDO NOT STAND OVER A RELIEF VALVE WHEN TANKPRESSURE IS HIGH. A relief valve’s purpose is to relieveexcessive tank pressure which can be caused by overfill-ing, improper purging of air from the container, overheat-ing of the tank, improper paint color, or high vapor pres-sure, to list just a few reasons. Check the tank pressuregauge if the relief valve is leaking. On a 250 psi design
44
TROUBLESHOOTING DOMESTICTANK FITTINGS (cont.)Relief Valves (cont.)pressure tank for example, if the relief valve is dischargingbetween the 240 to 260 psig range, the relief valve is work-ing properly as long as it reseats.A relief valve that discharges substantially below 240 psigor that does not reseat when the tank pressure is lowered,will have to be replaced. Do not attempt to force the valveclosed. Lower the tank pressure by withdrawing gas orcooling the outside of the tank.Always keep a rain cap on the relief valve to help keep outdirt, debris and moisture.Relief valves, like other pieces of equipment, will not lastforever. Fisher recommends that a relief valve not be usedfor over 15 years. Earlier replacement may be requiredbecause of severe service conditions or applicable federal,state, or local codes.Liquid Withdrawal ValvesA damaged seat or missing internal parts may allow anexcessive amount of liquid discharge when the closing capis loosened. These valves have a bleed hole in the closingcap to vent liquid before the cap is completely unscrewed.If a significant amount of the liquid continues to vent frombeneath the cap after 30 seconds, do not remove the cap.Should only vapor be leaking from under the cap, the con-nection to the withdrawal valve can usually be made.There is the possibility of liquid spray while opening thewithdrawal valve with an angle valve-special adaptor. Forthis reason, protective clothing should be worn and extremecare taken throughout the entire process.Service ValvesShow the customer this valve and tell him to shut it off ifgas is escaping into the house or any other abnormal situ-ation takes place. Check the stem seal and shut off seatsperiodically for leakage and replace them if necessary(empty the tank first).
45
sesaG-PLseiticapaCecifirOsaG-PL21elbaT)leveLaeStaRH/UTB(
ROECIFIROEZISLLIRD
ENAPORP ENATUBROECIFIROEZISLLIRD
ENAPORP ENATUB
800.0 915 985 15 135,63 414,14
900.0 656 447 05 248,93 861,54
10.0 218 129 94 163,34 751,94
110.0 189 211,1 84 389,64 362,35
210.0 961,1 623,1 74 880,05 387,65
08 084,1 876,1 64 692,35 024,06
97 807,1 639,1 54 146,45 449,16
87 080,2 853,2 44 922,06 082,86
77 926,2 089,2 34 963,46 379,27
67 942,3 486,3 24 590,17 995,08
57 185,3 950,4 14 429,47 049,48
47 911,4 966,4 04 920,87 954,88
37 876,4 303,5 93 315,08 512,19
27 180,5 067,5 83 127,38 219,49
17 594,5 032,6 73 068,78 506,99
07 573,6 722,7 63 702,29 235,401
96 439,6 068,7 53 213,89 454,111
86 318,7 858,8 43 571,001 665,311
76 023,8 334,9 33 797,301 276,711
66 848,8 130,01 23 583,901 700,421
56 559,9 682,11 13 340,711 986,231
46 535,01 349,11 03 911,431 640,251
36 521,11 216,21 92 663,051 664,071
26 537,11 403,31 82 103,061 827,181
16 763,21 020,41 72 085,861 411,191
06 800,31 747,41 62 716,571 290,991
95 066,31 648,51 52 916,181 698,502
85 333,41 942,61 42 828,781 539,212
75 620,51 530,71 32 697,291 765,812
65 275,71 129,91 22 053,002 131,722
55 939,12 278,42 12 525,502 799,232
45 036,42 229,72 02 996,012 368,832
35 967,82 516,23 91 549,322 088,352
25 508,23 091,73 81 664,332 376,462
BTU Per Cubic Foot = Propane—2,516 Butane—3,280Specific Gravity = Propane—1.52 Butane—2.01Pressure at Orifice, Inches Water column = Propane—11 Butane—11Orifice Coefficent = Propane—0.9 Butane—0.9
Reprinted from NFPA 54, Table F.2, 2002 ed.
46
LINE SIZING CHART
47
CONVERSION FACTORS
Multiply By To Obtain
LENGTH & AREA
Millimeters 0.0394 InchesMeters 3.2808 FeetSq. Centimeters 0.155 Sq. InchesSq. Meters 10.764 Sq. Feet
VOLUME & MASS
Cubic Meters 35.315 Cubic FeetLiters 0.0353 Cubic FeetGallons 0.1337 Cubic FeetCubic cm. 0.061 Cubic InchesLiters 2.114 Pints (US)Liters 0.2642 Gallons (US)Kilograms 2.2046 PoundsTonnes 1.1024 Tons (US)
PRESSURE & FLOW RATE
Millibars 0.4018 Inches w.c.Ounces/sq. in. 1.733 Inches w.c.Inches w.c. 0.0361 Pounds/sq. in.Bars 14.50 Pounds/sq. in.Kilopascals 0.1450 Pounds/sq. in.Kilograms/sq. cm. 14.222 Pounds/sq. in.Pounds/sq. in. 0.068 AtmospheresLiters/hr. 0.0353 Cubic Feet/hr.Cubic Meters/hr. 4.403 Gallons/min.
MISCELLANEOUS
Kilojoules 0.9478 BTUCalories, kg 3.968 BTUWatts 3.414 BTU/HRBTU 0.00001 ThermsMegajoules 0.00948 Therms
48
Multiply By To Obtain
LENGTH & AREA
Inches 25.4 MillimetersFeet 0.3048 MetersSq. Inches 6.4516 Sq. CentimetersSq. Feet 0.0929 Sq. Meters
VOLUME & MASS
Cubic Feet 0.0283 Cubic MetersCubic Feet 28.316 LitersCubic Feet 7.481 GallonsCubic Inches 16.387 Cubic cm.Pints (US) 0.473 LitersGallons (US) 3.785 LitersPounds 0.4535 KilogramsTons (US) 0.9071 Tonnes
PRESSURE & FLOW RATE
Inches w.c. 2.488 MillibarsInches w.c. 0.577 Ounces/sq. in.Pounds/sq. in. 27.71 Inches w.c.Pounds/sq. in. 0.0689 BarsPounds/sq. in. 6.895 KilopascalsPounds/sq. in. 0.0703 Kilograms/sq. cm.Atmospheres 14.696 Pounds/sq. in.Cubic Feet/hr. 28.316 Liters/hr.Gallons/min. 0.2271 Cubic Meters/hr.
MISCELLANEOUS
BTU 1.055 KilojoulesBTU 0.252 Calories, kgBTU/HR 0.293 WattsTherms 100,000 BTUTherms 105.5 Megajoules
CONVERSION FACTORS
49
FLOW EQUIVALENTS ANDTEMPERATURE CONVERSION
stnelaviuqEwolF41elbaT
wolfotsagfodnikenofoseiticapacwolftrevnocoTsagfodniktnereffidafoseiticapac
YLPITLUM:YB
yticapacwolfaevahuoyfISAGLARUTANni).cte,HFC(tnelaviuqewonkottnawdna
—foyticapacwolf
:enaporP:enatuB:riA
36.055.077.0
tnawdnaENATUBevahuoyfIwolftnelaviuqewonkot
—foyticapac
:enaporP:saGlarutaN:riA
51.138.124.1
ottnawdnaRIAevahuoyfIyticapacwolftnelaviuqewonk
—fo
:enaporP:enatuB:saGlarutaN
18.017.092.1
dnaENAPORPevahuoyfIwolftnelaviuqewonkottnaw
—foyticapac
:enatuB:saGlarutaN:riA
78.095.132.1
Table 15 Temperature Conversion
°F °C °F °C °F °C
-40 -40 30 -1.1 90 32.2
-30 -34.4 32 0 100 37.8
-20 -28.9 40 4.4 110 43.3
-10 -23.3 50 10.0 120 48.9
0 -17.8 60 15.6 130 54.4
10 -12.2 70 21.1 140 60.0
20 -6.7 80 26.7 150 65.6
The contents of this publication are presented for informationalpurposes only, while every effort has been made to ensuretheir accuracy, they are not to be construed as warranties orguarantees, express or implied, regarding the products orservices described herein or their use or applicability. Wereserve the right to modify or improve the designs orspecifications of such products at any time without notice.
www.FISHERregulators.com/lp
Emerson Process Management
Fisher Controls International, LLC.P.O. Box 8004McKinney, TX 75070 USATelephone: 1 (800) 432-8711
cOFisher Controls International, LLC., 2001, 2004; All Rights ReservedFisher and Fisher Regulators are marks owned by Fisher Controls International, LLC.The Emerson logo is a trademark and service mark of Emerson Electric Co.
HandbookD450116T01205/05 LP-10