lp-gas serviceman’s handbook

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

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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

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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.

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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


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

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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

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at m

ay b

e bu

ilt u

pon


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

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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


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


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.

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