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11·1J0HN ZINK : _ _ . JOHN ZINK COMPANY llO

Gl Gordon-Piatf Oil Piping

Information

INTRODUCTION: The information presented here is for the purpose of discussing the most common piping arrangements in

· boiler room piping and is not intended to be in con-flict with any code or agency.

Reference the following codes for compliance:

1. NFPA-31 Installation of oil-burning equipment

2. NFPA-8501 (formerly NFPA-85A) Single burner boiler operation

3. NFPA-8502 (formerly NFPA-85C) Prevention of furnace explosions/implo­sions in multiple burner boiler-furnaces.

Each of the above codes reference additional applica­ble codes for compliance. Some states and cities or insuring agencies have additional requirements due to the locality or environment.

Job sites can have piping arrangements that require special solutions that may or may not be discussed here. Some piping arrangements may present a poten­tial problem but in a given situation may be consid­ered minor and acceptable in lieu of a more elaborate system. Acceptance becomes the responsibility of the job site engineer or final authority.

Notes, comments and discussions are arranged in four separate areas:

A. General Statements. (Basic rules and com­ments relating to all forms of oil piping.)

B. Alphabetical referenced notes. (Relating to drawing where listed.)

C. Numerical referenced notes. (Notes that are common to some or all of the drawings or illustrations). Numerical notes begin on page 12.

D. How to use this material begins on page 14.

I

PIPING ILLUSTRATIONS - Figure 1 through figure 10. A. Figure l is typical of most job site piping

installations. B. Figure 7 through figure IO are fuel delivery sys­

tems to the boiler room piping. Depending on the burner fuel system and boiler room piping, the pumps illustrated can be a circulating, transfer or the burner pump.

C. Figure 2 through figure 6 are boiler room drawings. Any of the fuel delivery systems (fig­ure 7 through figure l 0) can be matched up with any of the boiler room drawings (figure 2 through figure 6) to illustrate a complete job site situation.

For example: Figure 2 can be combined with figure 7 to pro­vide a_n oil system with an overhead storage tank, circulating pump with a loop system to the burners.

GENERAL STATEMENTS: 1. Pipe

A. Use an approved pipe thread sealant. DO NOT use Teflon tape. (See Note No. 5.)

B. Use new pipe. Old pipe can contain rust, scale and dirt unless properly cleaned.

2. Pipe Threads A. Pipe threads should be per ANSI/ ASME

B1.20.1 (formerly ANSI B2.1).

i CAUTION ,

When joining threaded pipe or nipples to valves or control devices, and the end of the pipe is threaded too deep, the pipe will extend too far into the valve distorting the valve body and seating surfaces.

3. Copper Tubing A. Use copper tubing with flare fittings. B. Copper tubing does not contain rust or

scale. C. Copper tubing is easy to use, flexible and

will absorb vibration at the burner better than pipe.

D. Compression fittings are not acceptable. E. Sweat joints are acceptable providing the

. solder has an approved high temperature melting point.

4. Pipe Fittings A. Cast iron threaded fittings are not allowed

on oil piping. B. Fittings must have temperature/pressure

rating appropriate for the application.

5. Check Valves A. Swing or gravity lift type are acceptable. B. Check valves with composition seats suit­

able for fuel grade used seal better than metal seats.

C. Spring loaded check valves require pressure to open and may exceed allowable working pressure.

D. Valves must have temperature/pressure rat­ing appropriate for the application.

6. Manual Valves A. Gate or globe valves with non-nsmg stems

are difficult to visually determine their posi­tion.

B. Valves must have temperature/pressure rat­ing appropriate for the application.

7. Relief Valves A. When installed as a relief valve, divjde the

maximum spring range by 1.25 to deter­mine maximum set point.

B. Relief valves can serve as a combination relief/back pressure regulator where pres­sure sensitivity is a minor concern.

C. Diaphragm type relief valves normally fail closed. System requires additional relief protection.

8. Air in the System Air in the system can become a major problem if an accumulation is not prevented or con­trolled. All efforts to prevent or purge air from the system should be entertained. Fuel oil nor-

2

mally contains approximately 3% air. Air enters the oil by agitation in transit and spills. to the surface in the storage or supply tank when transferred from the transport vehicle. The most common source of accumulation is an air leak at some point in the suction line piping, fittings, valves, strainer, or flaws in a cast fitting. Air entrained or held in suspension can be as high as 10% if not properly recirculated or purged from the system. Air in the system can cause loss of pump prime or erratic pump outlet pres­sure.

9. Vapor Temperature/Pressure of a Liquid At a given temperature/pressure or vacuum; a liquid will vapor off or boil. Often a source other than No. 1 or No. 2 oil becomes available as a fuel for heating. Jet fuel (JP-4) is a good example since it contains a mixture of kerosene and gasoline. A suction line size normally acceptable for No. 1 or No. 2 fuel oil can have turbulent flow at valves, elbows and fittings. The high velocity through fittings with reduced ports can cause the lighter fraction (gasoline) to vapor off under vacuum.

A similar reaction can occur in heavy or resid­ual oils that contain lighter fractions or in a blended oil made by mixing No. 1, No. 2 oil or gasoline with heavy oil for the purpose of reducing viscosity for easier pumpability. When heated, the lighter fractions can vapor off (boil) with a few inches of vacuum. Oil vapor entering the pump has the same effect as air.

A pump and heater set is sized to deliver heavy oil under pressure at 200°F to a multiple boiler installation. With only one burner operating, the excess capacity of the pwnp and heater set is returned to the supply tank. lf this process is allowed to continue,. in time the supply tank will be 200°F. Do not 'heat oil above flash point except under high pressure. (Ref. Figure 6)

I 0. Viscosity When heated heavy oil is the prime or only source of fuel for heating, a back-up system should be considered. An unplanned shut down can allow the supply tank and suction lines to cool beyond pumpability and the system can­not be restarted.

I

\.;.)

r VENT RETURN BENO ~

APPROVED METAL SCREEN --------.___ ~

VENT PIPE

PLAIN CAP or LOCK FILL CAii'

,;;:--- WATER TIGHT CAP FOR GAUGE

,..

....___ WALL MOUNTED ----..._ TANK GAUGE

ANTI-SIPHON VALVE

GROUND LEVEL \ STICK ANO CLEAN OUT PIPE

A'· I H~ ~

FILL PIPE TO CURB GR.ADE ooWN T_Q TAl'l_lS.

(F.O.S.) FUEL OIL SUPPLY I I I <-..

(F.O.R.) FUEL OIL RETURN ---+-1--+--... (Note No. 2)

ANCHOR TO CONCRETE

3'

INOTESI ~1 Alphabetical (Numerical Notes Begin on Page 12)

FIGURE 1

BURNER

OIL PUMP

(NoteB) (Note No. 9)

OIL STRAINER (Note No. 5)

BURNER

Burner Pump(s) Drawing its Supply from the Supply Tank

(See Note No. 4)

A. Supply tank shown is for illustration ONLY. Reference NFPA 31 and local codes for tank installation.

,.,

OIL PUMP

(Note B) (Note No._9)

B. In multiple burner installations where the burner pump (mounted or remote) draws its supply directly from the supply tanks; each pump should be provided with a separate suction line whether the tank is above or below the burner pump. A common return line is acceptable if its size is based on the total suction capacity of the burner pumps.

C. If a single suction supply line is available from an existing supply tank, then a circulating or transfer pump should be considered.

D. Piping as illustrated becomes overhead suction lines since a portion of the supply tank is above the piping in the boiler room (Ref. figure No. 9). If the supply tank is below the boiler room and with piping as illustrated then reference figure No. 8.

"

ex, C 3 C1> ., ,, C 3

"C -t/1 -C. ol ~ 5· (0

::;: t/1 en C

"C "C '< C a· ~ '< ~ 0 3 -::r C1>

en C

"C "C '< ;t :::, ~

.,.

'-,'

FIGURE 2

} ~I

r OIL STRAINER / _ (Note No. 5)

tui q ... '"11----i-' \ II ~i (Note No. 9)

'- ---4V \ II

OIL STRAINER (Note No, 5)

tui ~ ~i (Note No, 9)

i.. r"LR GATE I ,JII VALVE

~ CROSSOVER PIPING

'---------------------- FLOOR TRENCH ______________________ __.

(lfu1ed)

Boller Room Piping with Circulating Loop below the Burner Fuel System (See Note No. 4)

Numerical Notes Begin on Page 12.

~' ~-.. '

0:, 2. c6" .. g 3 "CJ ;s· s·

C0

~ ~ (") ~-c ;--:i'

C0

~ 0

"O 0:, ft)

I -:r ft)

0:, C 3 ft) .. 'T1 ; -en

l

v,

~

FIGURE 3

CHECK VALVE

,.,

AIR-+ { (:J ~ ~ AIR TRAP (Note A) ,,----- CROSSOVER PIPING ---....

ai ci ..:

i

GATE VALVE

CHECK VALVE

(Note No. 14)

INOTESI

t <Ii q u.

CHECK VALVE

(Note No. 15)

.t ai q u.

F.O.R.

F.Q.S. C..olL

CHECK VALVE

(Note No. 15)

Boller Room Piping with Circulating Loop above Burner Fuel System (See Note No. 4)

Alphabetical (Numerical Notes Begin on Page 12)

t ai q u.

r,

(Note No. 13)

A. An air trap at the end of overhead circulating loops allows air to rise into the vertical pipe and be forced to return. Piping can be as illustrated or the end of the final section of pipe elevated slightly to produce an air trap.

~

c:, 2. ;-., :;o 0 0 3 "tJ -a· 5·

(Q

:IE ;:;: ':I' C') ~-c ;­~ = (Q

r-g "0

> C" 0 < CD -':I' CD c:, C 3 CD ., -n C CD -tn

'< ;-3

°" I

CHECK VALVE ~-

AIR-I □ Bf? ( F.O.S. VACUUM BREAKER --+

(Note No. 12) -

OLS~ES7 (Note No. 5)-

(NoteB) BURNER

R~ II I I ~ ~-

TI I I TI GATE I I 11 \ '-'WIVALVE 'c..'J:O I JI I I J.l ~R.

SUPPLY GATE ~7 --+ VALVE CHECK F.O.R. VALVE

(NoteA)l] I (Note No.15)

~- -- F.~ CHECK VALVE (Note No. 14)

I

I

Boiler Room Piping with Circulating Tank and Overhead Supply and Return Lines

(See Note No. 4)

INOTESI

Alphabetical (Numerical Notes Begin on Page 12)

A. Each burner pump should be provided with a suction line of its own.

I

B. A common return line is acceptable provided it's size is based on the total suction capacity of the burner pwnps it serves.

4-, '-'

FIGURE 4

I (Note No. 13)

OIL STRAINER (Note No. 5)

B

I l 111\W [)II I GATE VALVE

CHECK VALVE

(Note No.15)

'-,·· ...

0 < CD 3-CD I» C. t.n C

"C I "C '< I» :, C.

s' -C 3 ,-c 5· CD en

r

FIGURE 5

......i

I SUPPLY GATE VALVE

INOTESI

OIL STRAINER (Nole No. 5)

,., MULTIPLE AUXILIARY OR DAY TANK INSTALLATION

VENT-----~ (Note A)

3-WAY CONSTANT LEVEL FLOAT CONTROL

~- BACK PRESSURE REGULATOR (If required}

VENT ~~ (Note A)

11

LIQUID~ LEVEL CONTROL

/

AUXILIARY TANK

Sl=O=I I : .. ~~ ... : ; IO ~- (NoteC}

(NoteC)

F.O.S .•

(NoteB}

F~

Boiler Room Piping with Auxiliary Tank (See Note No. 4)

Alphabetical (Numerical Notes Begin on Page 12)

A. Vent back to top of supply tank or outside of the building in an approved manner.

OIL STRAINER (Note No. 5)

BURNER

B. Each burner pump should be provided with a suction line of its own. C. A common return line is acceptable provided it's size is based on the total suction capacity of the burner pumps it serves.

('

GATE VALVE

c:, 2. ;-.., :::0 0 0 3 "tJ -6' 5'

(Q

~ ~ > C ~--Di' '< ~ :::, ~

00

TEMPERATURE GAUGE

INOTESI

FIGURE 6

GATE Vf>J.VE

OIL PREHEATER (II Used) (Note B)

Boiler Room Piping No. 2 Thru No. 6 Oil Air/Steam Atomizing

,+- F.O.R.

CIRCULATING LOOP

F.O.S,__.

STRAINER

t ct! q ...

.,; ci u:

i

Alphabetical (Numerical Notes Begin on Page 12)

A. The diverter valve can be a globe, gate or (BPR) back pressure regulator valve that operates in coordination with the BPR at the end of the circulating loop. This is for the purpose of directing the excess capacity of the delivery pump back to the supply tank before it enters the oil preheater. Reference "Vapor Temperature/Pressure of a Liquid" under general statements. A temperature gauge installed in the return line will indicate an acceptable return line oil temperature.

8. Oil preheater is not required with No. 2 oil and depending on locality it is not required with No. 4 oil. Oil preheater is required for No. 5 and no. 6 oil.

C. Oil trim heater not required for No. 2 oil

D. There are two systems illustrated.

(BPR) BACK PRESSURE REGULATOR Vf>J.VE

GATE VALVE

~ II

111 111

,---- (Note D)

RELIEF/REGULATING 7 r; COMPOUND VALVl;: .. (Note F) VACUUM/PRESSURE ,,· ·,;,. GAUGE

"'/:>' ' ~:: CHECK PRESSURE · · v'i.tve· n r REDUCING r. F.O.R. ~ ~ VALVE

-- ,.. (II Used)

TO BURNER FUEL SYSTEM

OIL PUMP

I. The pump at the supply tank delivers oil to the BPR at the end of the circulating loop. The BPR maintains pressure to the burner fuel system. This arrangement does not require a burner pump.

2. Fuel systems equipped with individual burner pumps. The BPR at the end of the circulating loop maintains pressure to the burner pump or pressure reducing valve. The excess capacity of the burner pump over the firing rate is returned through the relief/regulator valve.

E. Do not install manual (stop) valves in return lines.

F. Reference 7-B under General Statements.

"-· ~ ~

0:, 2. c6" ., g 3 -a -6' 3·

cc z ~ N -:::r 2 z ~ 0,

g ~ :::!. CJ) -CD Al 3

~ 3 N' 3'

cc

..

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Figure 7 Fuel Delivery System by Gravity Feed from an Over Head Supply Tank

(Note No. 2)

MAXIMUM STATIC HEAD

(Note A)

I

lNOTESI Alphabetical

GAT~ VALVE

PLUGGED TEE ~ (Nole B) . 't

t a: ci u.:

VALVE

Oil

COMPOUND VACUUM/PRESSURE

GAUGE

(IF REQUIRED) .2-0.R.

GATEj OPTIONAL POINT STRAINER Oil

OF RETURN (Nole No. 5) PUMP (Note No. 6) (Note No. 8 & 9)

Fuel delivery by Gravity Feed from an Overhead Supply Tank

(Numerical Notes Begin on Page 12)

A. A normally closed (NC) pressure reducing valve (PRY) is required to prevent oil from the supply tank to gravity feed into the boiler room in case of an open or broken line. Pump vacuum opens the valve allowing oil to flow.

Valves produced by Webster heating products (Model OSV) and Suntec (Model PRY) are available for small capacity units with No. 2 oil or lighter. Reference their data for installation and capacities.

For greater capacities and higher viscosities a similar valve is required. If the valve (PRY) is not a pos­itive shut off type (No leakage allowed) then the maximum static head is limited to the pumps positive pressure inlet conditions.

B. A plugged tee is required to purge air from the static head below the PRY.

9

-Figure 8 Supply Tank Below the Boiler Room Piping

VACUUM BREAKER (Nole No. 12)

CHECK VPL.VE ._ F.O.R.

PLUGGED TEE -----.. (NoleB) .....

MAXIMUM SUCllOH

LFT (NoleD)

CHECK F.O.S.► VALVE

,(NoleB)

STATIC Hl:AD

FRICTION

'' , '

--- HEAD ---.

I '1 :: ·•, •' :,

..... ,!t ,.. . .. ··• •' I 1' ,, ,.

•' ,, ,. ,, ,• ,, ,. ,• ,.

(Nole C)

,• •' •' •' ::, ©

~------~:~

OPTIONAL POINT OFRET\JRN (NoleNo.6)

...---- COMPOUND

OL STRAINER (Nole No. 5)

VACUUM/PRESSURE GAUGE

(IF REQUIRED) F.O.R. ._

Fuel Delivery System with Overhead Suction Lines and Supply Tank below the Boiler Room Ftping

Alphabetical (Numerical Notes begin on Page 12.

A. A check valve installed in the horizontal piping will prevent oil from flowing back to the tank during the purging of air proce~ure. Periodic manual pwging of air is required.

B. A plugged tee installed at @) for purging air from the overhead suction line. (See Note A)

C. With air purged from the suction line between @ and@, the static head betweea @ and ® will offset an equal height of suction lift between @ and {g. Under these condilions_ the ()nly energy (vacuum) required of the pump is the friction loss of the suction live between@ llftd @.

Air entrained in,the oil .and \llnt'ler vaauum between ,.@ and @ will aq,and and collect in the hori­zontal piping between {Q and @. i.See "Air in the ~em") A-s air continues to accumulate, it will move into the vertical piping below Q?) displacing the oil and lower the static head. Pump vacuum will increase in relation to loss in the static head and vacuum will increase as the liquid level of the tank drops.

~sign conditions should not exceed the pumps suction lift capacity between @ and © plus the friction loss of the suction line piping and the vapor temperature/pressure of the liquid.

D. The suction lift between @ and @ changes depending with the tank fill.

10

..

J

C

Figure 9 Fuel delivery System with Supply Tank Above the Boiler Room Piping

MAXIMUM SUCTION

LIFT

CHECK VALVE

(Note No. 1)

,,; 6 u:

t a: 6 u:

PRESSURE GAUGE

(Nole No. 13)

~----- COMPOUND VACUUM/PRESSURE

GAUGE

(IF REQUIRED) _.!:.OR

.l'@ ~----~

!NOTESI Alphabetical

STATIC HEAD

OPTIONAL POINT OF RETURN (Nole No. 6)

FUEL DELIVERY SYSTEM WITH SUPPLY TANK ABOVE THE BOILER ROOM PIPING

(Numerical Notes begin on Page 12)

A. When any part of the supply tank is above the lowest point of the suction line piping in the boiler room, an anti-syphon valve is required. This prevents siphoning of oil into the boi_ler room in case of an open or broken line. The valve should be installed at the highest point in the suction line piping. Refer to the manufacturer's instructions for proper installation, purging of air and testing of the anti-syphon valve.

By design, a spring that is equal to the static head below the valve holds the piston or poppet on its seat. Pump vacuum lifts the piston against the spring, allowing liquid to flow. Increased capacities require higher lifts against the spring with an additional increase in pump vacuum.

For the purpose of discussion, install a test tee with a bleeder valve at @. Supply tank should be filled and air purged from the suction line between @ and @. Open the bleeder valve. If oil flows, then a stronger spring is required in the anti-syphon valve.

If the stronger spring installed is greater than the static head, then pump vacuum will increase equal to the excess spring pressure.

Reference "Air in the System" and "Vapor Temperature/Pressure of a Liquid" under General Statements. Air entrained in the oil and under vacuum between @ and @ will expand, escape from the oil and collect in the horizontal piping between @ and (g. As the accumulation of air continues, it will move into the vertical piping below the anti-syphon valve at © displacing the static head. Pump vacu­um will increase in relation to the loss in static head. Static head below the anti-syphon valve does not offset the suction lift. Pump vacuum will increase as the liquid level in the tank drops.

B. A check valve installed in the horizontal piping will prevent oil from flowing back to the tank during the purging of air procedure. Periodic manual purging of air is required.

ll

1gure Fuel Delivery System from a Supply Tank Below the Boiler Room Piping

(Nole No. 2)

' ' .. ' ' ' '

OI.. PUMP

(Nole No. 8 & 9)

(IF REQUIRED) .,_!;0.R.

' ' ' ' ' ' ' .. Fuel Delivery System from a Supply Tank

. below the Boiler Room Piping

NOTES: NUMERICAL I. Do not install manual (shutoff) valves in return

lines. Check valves are acceptable and required if any part of the supply tank or lines are above the burner fuel system or lowest point in the piping. This prevents siphoning of the oil into the boiler or boiler room in case of an open or bro­ken line. Install the check valve at the highest point in the horizontal piping and as close to the supply tank as practical.

2. The return and suction lines should be spaced apart, or the return line spaced higher in the t.ank than the suction line, to prevent air from the return being drawn into the suction line and recirculated. (See note #7)

3. A check valve in the suction line is·· required if the supply tank is below the burner, circulating or transfer pump to assist in priming or lu,lding prime in the off cycle. The check valve should be installed as close to the tank as practical. Foot valves in the t.ank are not advisable.

4. Burner can be any model (R-S-F-FL) with fuel sys­tems for pressure or air/steam atomization of No. 2 oil. F and FL models do not provide for burner mounted pumps. See piping illustration figure 6 for alternate methods. The air/steam atomizing source is not shown. Ref. l-gen-80.xx for fuel system used.

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5. A clean supply of oil is essential. It must be free of entrained debris that can plug orifices or become trapped under seats of valves and control devices .

. Oil strainers are supplied as standard on remote pump sets. Burners supplied with mounted pumps require external strainers to be inst.ailed with metal wire mesh or perforated baskets. The basket open­ing should be smaller than the smallest opening in the fuel system. Simplex nozzles have an integral wire mesh strainer and requires periodic mainte­nance. Paper or cloth type filters are not accept­able on any burner fuel system. See "Pipe .. under general statements.

6. Where the length of the return Jine andlor t"he height of lift to the top -of the tank produces a retum line ;pressure unacceptal>le to iihe bumer fuel .system ,or pump inlet conditions; the optiomd point of return may be considered.

--------' WARNING! ,

When the optional point of return is used, then the circulating loop becomes a closed circuit. The return to the top of the tank is omitted. Purging of air will be through the burner nozzle and the vacuum on the suction side of the cir­culating pump wilt be imposed on the circulat­ing loop. (See note No. 7 and No. 13)

C

7. Air or vapor in the suction line displaces the oil, reduces the pumps capacity, pressure and burner fir­ing rate.

8. Circulating and transfer pumps should be installed as close to the source of supply as possible and sized as follows: A. If the excess capacity of the burner pumps

is returned to a stand pipe, circulating tank, aux­iliary tank, day tank or circulating loop and remains a source of supply to the burn­er pumps; the capacity of the circulating or transfer pump is 1-1/2 times the total firing rate.

B. If the excess burner pump capacity is returned to the source of supply and not available to the burner pumps by recirculation (for example, a circulating loop with a back pressure regulating valve) size the circulating pump equal to or greater than the total suction capacity of the burner pumps.

C. Burners without individual burner pumps where a back pressure regulator valve at the end of the circulating loop maintains pres­sure to the burner fuel system, size the sup­ply pump 1-1/2 times the total firing rate.

9. Burner Pumps (Mounted or Remote) sized 1-1/2 times the firing rate for by-passing oil systems and for desired firing rate for all other systems.

10. For circulating loops piped in a manner where the excess capacity of the burner pump(s) is returned to the circulatin_g loop, then the circu­lating loop becomes a reservoir to the burner pumps by recirculation. The return line should be installed above the supply line. High veloci­ty in the oil lines can pmduce turbulent flow that will hold air in suspe'DS101'l and r.emam entrained in the oil. Reduce the velocity by increasing the circulating loop pipe size to 'give fhe air time to rise to the top of the run and escape thr~h the crossover piping. Burner pumps can bw oil purged of excess air at the bot­wm -0f'the rnn. See Table 1 for laminar flow piping with No. 2 oil.

11. Long horizontal suction lines can have high points in the piping that will become air traps. When the pump starts, the column of oil between the pump and supply will not instantly accelerate to equal the pumps capacity and a vacuum higher than under normal operating conditions will occur. Air will expand and escape from the traps. If the volume of air is equal to or greater than the internal capacity of the pump, the pump will lose its prime.

13

12. A job site layout can have a situation where there is an extreme distance between the height of the piping in the boiler room and the bottom of the supply tank. The weight of the oil falling through the return line can produce a unstable condition in the circulating loop and/or the burner fuel system. Install a vacuum breaker ( check valve) at or near the height of the return line. Vent air from the top of the supply tank or from outside the building in an approved manner.

13. Excessive pressure on the burner fuel system can be produced by job site conditions or piping arrange­ments. A. pressure produced by overhead piping as illus­

trated in Fig. 3 and Fig. 4. B. Friction loss of return lines plus static head to

top of supply tanks installed above the fuel sys­tem as illustrated in Fig.7, Fig. 8 or Fig. 9.

Some fuel systems employ a spring loaded one way oil cylinder to actuate the air control. Excessive return line pressure produced by A or B above can hold the cylinder in the extended posi­tion. For a satisfactory performance of these fuel systems, the return line pressure should be limited to 3PSIG. Alternate fuel systems may be available or ref. the boiler room piping illustrated in Fig. 5.

When pressures produced by A or B above exceed the inlet pressure of the burner mounted pump; change the system to a remote pump with an accep­table inlet pressure or ref. Fig. 5 for boiler room pip­ing. Ref. "Pressure from Overhead Piping" on page 15.

14. Discharge check valves are supplied as standard equipment by design on duplex pump sets. Discharge check valves on simplex pump sets are not required When a circulating or transfer pump has discharged to an extreme height (for example to the roof of a building) and is in the off cycle; the pressure produced by the static head could exceed the pump inlet conditions if the oil flowing back through the pump cannot return to the tank. A dis­charge check valve will be required if not supplied.

15. The arrangement of some burner fuel systems can allow oil from the return line to flow back through the fuel system and nozzle into the boiler when the burner is not on demand. Check the fuel system to see if a check valve is supplied or required.

How to use this material - The information presented herein requires additional reference material. For exam­ple, many references are made concerning the pump inlet conditions. This type of information will be found in separate catalog sheets. Pump sets for light oil, high pressure atomizing, reference catalog sheet 6-10-2.2, Rev. 5 or later. For light oil circulating or transfer pump sets, reference 6-10-2.3, Rev. 7 or later. For heavy oil systems, reference 6-10-2.31, Rev. 5 or later. The burn­er fuel system will also need to be referenced. These can be found in catalog sheets l-gen-80.xx.

How a pump works - The term "suction lift" is often used in reference to the distance or length of pipe below the inlet port of the pump. Technically, we do not "lift" a liquid. On the average, at sea level, there is 14.7 PSIA atmospheric pressure (29.9" Hg vacuum). Atmospheric pressure decreases at higher elevations. It is not practi­cal (cost) to build pumps to develop a complete vacuum (29.9" Hg). By design, we can only use about half of the atmospheric pressure, 7-1/2 PSIG or 15" Hg.

When a pump starts, it removes the air from inside the pipe and reduces the pressure below atmospheric pres­sure at the pump inlet port. This is normally registered by a vacuum gauge in inches of Hg. [Divide in. Hg by 2.034 to determine PSIG (gauge pressure)]. It is the dif.:. ference between the reduced pressure (PSIG) at the pump inlet port and the atmospheric pressure (PSIA) available that pushes the liquid through or up the pipe.

Positive displacement gear type pumps require a close tolerance between the gears and housing for thin liq­uids. Pressure at the discharge side of the pump causes the thin liquid to flow (slip) back past the gears to the inlet side. High viscosity liquids require increased gear clearance to allow room for the thicker fluid. For high viscosity liquids, the pump RPM is reduced through a V-belt drive or gear reducer to allow time for the thick­er fluid to fill the space between the gears without cav­itating. With this reduced pump RPM and· increased gear clearance, the pumps lose their ability to deliver in capacity and pressure of light oil. Where customer requirement is for multifuel grades (e.g. No. 2 thru No. 6) a separate fuel pump designed for light oil is required.

Equivalent line length - Equivalent line length includes the measured length of the run plus the friction loss in equivalent length of valves, fittings, etc. installed in the suction, discharge or return line piping. (Ref. Table 6)

Horizontal suction and discharge lines - On installa­tions where suction lift is not required, use the upper portion of the charts (Chart I thru 7). Suction line sizing should be based on the suction capacity of the pump.

14

Example #1: On the 750 SSU chart (Chart 5) a 100 foot line flowing 4 GPM will intersect at the· 1-1/4" pipe size. When 3 points intersect (GPM, Line Length and Pipe Size), the pump requirement will be 5 psi dis­charge pressure or IO" Hg vacuum on the suction side.

Now check the velocity. Move horizontally to the right on the 4 GPM line to the 1-1/4" NPS velocity chart. The velocity in ft/sec. is .86. Ref. Table 7 for maximum rec­ommended velocities and find that .86 ft/sec. is well within the limits for 4 GPM in 100 ft. of 1-1/4" Sch. 40 ptpe.

Example #2: Again on the 750 SSU (Chart 5) a 20 foot line is flowing 20 GPM and intersects at the 1-1/4" NPS. The velocity is 4.29 ft/sec. On Table 7, the 4.29 ft/sec. exceeds the recommended velocity on the suc­tion side (3.3 ft/sec.) but is acceptable on the discharge side (5.6 ft/sec.). High velocity occurs in shorter suc­tion and discharge lines.

When sizing suction lines, DO NOT exceed the recom­mended velocity. For example: On the 5000 SSU (Chart 7) and (Table 7), for maximum recommended velocities by viscosity, a 30 ft. suction line flowing I 0 GPM of 7500 SSU oil will intersect at the 2" pipe size. Move horizontally to the right and find a pipe size with an acceptable velocity for 7500 SSU (.5 ft/sec.). A 3" pipe size would be required.

Suction lines with lift - For Suction lines only, use the lower portion of the charts (1 thru 7). Note that the chart line sizing is based on IO in. Hg vacuum with no lift and progresses to 15 in. Hg at 15 ft. of lift.

Example: Reference chart 6 for 2500 SSU. A suction line with an equivalent length of 60 ft., I 5 ft. of lift and flowing 7 GPM will require a 3" pipe size.

In the above example, a major portion of the pumps suction .. ability has been consumed in static lift and a small portion remains for friction loss. We cannot change the static lift requirement, but we can change the friction loss per foot by increasing the pipe size. For the 3" pipe size, velocity is not a concern, but the increased pipe size will require a larger strainer than listed on the catalog sheets for pump sets as a standard. A pipe size larger than 3" in this example would be of very small value.

Oil Strainers - Strainer sizes listed on the catalog sheets for pump sets and included on standard material lists are sized by velocity for the purpose of pricing since job site conditions are unknown. Strainers one line size smaller are also acceptable unless they pro­duce an equivalent suction line length that is unaccept­able due to the job site layout. For best results, select a strainer that is the same as the adjusted suction line size.

,,

C

C

L

Suction Line Piping using friction loss Tables 2 tbru S. -

Example 1: A pump with a suction capacity of7.5 GPM of No. 6 oil at 5000 SSU in a 2" suction line with an equivalent length of 35 ft. What is the vacuum required at the pump?

Line Length x Friction loss/ft (table 5) x sp. gr. (chart 7) = psi

35 X .123 X .97 = 4.18 psi

Convert psi to in. Hg.

4.111psi x 2.034 =•8:5in Hg.at.the pump

The velocity for 7.5 GPH (Chart 7) in a 2" pipe is (by interpolation) 0. 7 ft/sec., ref. Table 7 for maximum rec­ommended velocities at 5000 SSU on the suction side of the pump. (.85 ft./sec.)

Example 2: A 50 ft. equivalent length of 3/4" type-K copper tube horizontal suction line exists from the tank to the burner pump. The new pump has a suction capac­ity of 9 GPM of light oil and a maximum suction capa­bility of 10 in. Hg. Will the 3/4" line supply the pump?

C . H . IO" in. Hg 4 91 · onvert m. g to psi 2

_034

= . pst

Ref. Table 2: A 3/4" line flowing 9 GPM has a friction loss/ft. of 0.1063 psi x 0.86 sp. gr.= .0914 psi/ft.

Solution:

4.91 psi _ . . · L. Le h f

. . Lo sift. 0 0914

. - 53.7 ft. Maxmmm Suction me ngt . nctlon · s . psi

Suction line is acceptable for 10 in/Hg pump capability but the velocity is high. Chart 2 indicates a velocity of 7 ft/sec and table No. 7 recommends a maximum velocity of 5 ft/sec of 40 SSU oil on the suction side.

Discllvge Lines with-Static Head -

For uample: A 75 ft. equivalent length discharge line flowing 5 GPM of 2500 SSU oil in a 1-1/4"' Sch. 40 pipe with 12 ft. of lift to a back pressure regulator set at 100 psi. What is the pressure required at the pump?

75 ft. x sp. gr. x fiiction loss/ft. 75 x .93 (ref. Chart 6) JC0.207 (ref. Table 5) =

12 ft. lift x static head in psi/ft. 12 x .404 (ref. chart 6) =

BPR set at 100 psi

Total pressure at pump=

14.44 psi

4.85 psi

100.00psi

119.29 psi

Now check the velocity. Ref. Chart 5, 6 or 7. Any chart will work when the GPM and pipe size. in the velocity charts match up. 5 GPM in a 1-1/4" sch. 40 pipe has a velocity of 1.07 ft/sec.

Pressure from overhead piping - The static head in psi/ft. given in Charts 1 thru 7 is based on the sp. gr. listed in each chart and is intended for use when the actual sp. gr. is not known. For Hample - Ref. the viscosity/temperature chart on page 24. A fuel oil with a viscosity of 2500 SSU could be any fuel grade of 4, 5 w 6 depending on temperature and the sp. gr. would not ~w~s be 0.93 as .shown on chart 6.

15

Use the following to determine the weight of a liquid when the sp. gr. is ·known:

27.r we (1 psi) = inches in liquid column to= 1 psi sp. gr.

1 psi in. liquid column = psif111. of liquid column x 12

= psi/ft. of static head.

Reference note No. 13.

Sizing Circulating Loops - For this discussion, ref. boiler room piping fig. 2 and fuel delivery system fig. 7. Run copies and match them together to illustrate a complete job site situation.

Example: Four boilers with burners firing 35 GPH each on No. 2 oil requires a 210 GPH circulating pump set (4 x 35 x 1.5 = 210 GPH/3.5 GPM). Ref. Note No. 10 and Table 1 for piping at laminar flow. A circulating loop with 3.5 GPM capacity requires a 1-1/4", Sch. 40 pipe to reduce the velocity to laminar flow.

Piping between the circulating pump and the circulat­ing loop can be sized by standard calculation or ref. Charts 1 thru 3 for sizing with an acceptable velocity.

Other Considerations - Heavy oils, especially resid­ual heavy oil, tend to leave a deposit on the walls of the pipe reducing the internal diameter: increasing ~eloci­ties and friction loss. Consideration should be given to adding 20% to the measured length of the suction li_ne. Some codes require threaded piping inside boiler rooms to be sch. 80. Add 10% to the measured length of the suction line for this portion of the piping.

°'

SCH. ,o PIPE COPPER TUBE • TYPE K COPPER TUBE

I MECHANICAL TYPE NOMINAL

SIZE f MAXIMUM VELOCITY MAXIMUM VELOCITY MAXIMUM VELOCITY ■

GPM FTJSEC. GPM FT./SEC. GPM FTJSEC. I

1/4 . . .. 0,77 3.388 0 ..... 7 5,733 I 3/8 1.24 2.09 1.02 2.587 0,770 3.388 1/2 1.57 1.88 1.33 1.959 1,081 2.,02 5/8 . . .. 1.72 1,854 1,405 1.859 3/4 2.08 1.25 1.88 1.387 1.720 1.517

2,65 .98" 2.51 1.037 2.35 1.1096 1-1/4 3.49 .748 3.14 ......... . . .. 1-1/2 4.06 ,640 3.74 ,6969 . . ..

2 5.23 .500 . 4.98 ,5297 . . .. 2-1/2 6.24 ,418 6.15 . 4238 .. ..

7.74 • 336 . . .. .. . . .15 . 258 . . .. .. ..

There is a very narrow margin between laminar and Reference the above table for circulating loops turbulent flow. No. 2 oil will become turbulent with where air in the system presents a problem and sue-capacities greater than those given in the above tion lines with liquids that contain lighter fractions table. such as gasoline or alcohol that will vapor off under

vacuum.

GPM

0.5

I 1.0 I .0180 ! ,90Zl I _ I I I LAMINAR FLOW 1_._5 n.1.11n n11n nn,~ Note 1 11----11

2.0 2.5 3.0 3.5 4. 4.5 5.0 ,Q030 J)014 §.,0 0040 .0020

I

I

GPM

v,v

1,2 . .,

3.5 4,0 4.5 5.0 6.0 7.0 8.0 9.0 10.0 12.5 15.0 17.5 20.0 25.0 30.0

GPM

0.25 0.5

0.7~

y 2.0 2.5 3.0

4.0

11,,---i- 3/8 I 1/2 I ,v,v .... ,v.,, .......

I :fiH t 1HH I •iili 1 t1•.1t:'1

• 378" .1035 _.47Rtl .1313 , .. .,.,n ,1819

,1953 _2701

HIGH VELOCITY

Note2

5/8 I 3/ .. I 1 I 1-11"

,OOH I ,2oa~ I I I LAMINAR FLOW

""·· '"'" .. Note 1

,037 .. .0198 --

.00,9 .0,15 .0251 .0083 .0022 -.0585 ,0309 ,0078 ,0027 .00 .0706 .0373 .0094 ,0032 .0014 ,0978 .0516 ,0129 ,00 .... .0019 .1285 .0879 .0170 .0056 .0025 ,1829 .0862 .0216 .0074 .0032 .2009 .1063 .0266 .0091 ,0039 ~ ,1282 .0321 .0110 .0041 ,'IR'17 19n7 .0478 .0184 .007

,71138 .0882 .0227 ,0098 .0780 .0298 .0130 110, ,0378 .01

,111-'7 .0583 .02,5 .0778 .0339

7.0 .74i0 ,0050 .0026 ,0008 I 4,5 I I HIGH 5,0 VELOCITY , •v•v ,vv,, ,v •-v _M_ Note 2 I I I ~••• I n1,.... I ..... ., I 8.0

9.0 10.0 12.5 15,0 I 17.5 I I HIGH 20.0 VELOCITY 25,0 Note 2 30.0

.0070

.0080 ,0100 mo .O_UQ .0280 .0350 .0520 .0720

INOTl!SI I. Friction loss shown above the upper heavy line is at laminar flow. See Table I.

'-'

.0033

.0040

.0049

.0073

.0100

.0130

.0170

.0250

.0350

.0010

.0012 ,0014 .0022 .0030 .0040 .0050 .0078 .0104

7.0 8.0 9.0 10.0 12.5 15.0 17.5 20.0

2. Friction loss and capacities below the lower heavy line exceed the maximum recommended velocity in ft/sec. Ref. pipe sizing Chart 1 thru 3 and Table 7 for No. 2 oil.

~

3. Multiply the above friction loss values by the specific gravity (s.g.) to detennine the correct friction loss. No. 2 oil has an average s.g. of 0.86. No. I oil has an average s.g. of 0.83.

~ > '

---.J

,.... r,

IF.l-•~-,~-•••• •-.::,"~ ~Ttlt rrir.__.,U■ !.11 •I~

PIPE VISCOSIT't' IN SSU/CS GPM SIZE 200/43 500/110 750/195 1500/330 2500/550 3500/770 5000/1100 7500/1848 10,000/2198

3/8 0.099 0.25" 0.380 0.781 1.288 1,770 2.535 3.800 5.085

0.5 1/2 o, ... 0.100 0.1~0 0,-mu 0.500 o 700 1.000 1 500 2 ....... 3/4 0.013 0.032 0.049 0.097 0.1,2 0.227 0.325 0.487 0.849 1 0.005 0.012 0.019 0.037 0.0,2 0.017 0.124 0.185 0,274

1/2 0,078 0.200 0.304 0,800 1,000 uoo 2.000 3.000 4.000

1.0 3/4 0.025 0,085 0.097 0,195 0,325 0.454 0.950 0,974 1.300 1.0 0.100 0.025 0.037 0,074 0,124 0,173 0.247 0.370 0.41M

1-1/4 0,003 o.oo, v.v 1, 0,025 o.- O,unn 0,083 0.124 0.185 1/2 0,158 0.405 0.100 1.200 2.000 2.100 4.000 e.ooo 8.000 3/4 0,051 0_130 0.1115 n •-• 0,850 0 910 1.-.... 1.950 2.600

2.0 1.0 0.019 0.049 0.074 0,1"8 0.274 o.34e 0.495 0.742 0.989 1-1/4 0.008 0.017 0.025 0.050 0.013 0.11, 0.195 0.248 0.330 1-1/2 0.003 0.009 0.013 0,u4t 0.045 0.082 0.089 0.134 0.178 3/4 0.078 0.195 0.290 0.515 0,975 1.395 1.950 2920 3.900 1.0 0.029 0.074 0.111 0.223 0.371 0.520 0.742 1.110 USO

3.0 1.114 0_010 nw,• nn o_u,.a n .-,. 0_173 0_24a n ,70 0498 1-1/2 0.005 0.013 0.020 0.040 0.087 0.094 0.134 0.200 0:287 2.0 0.002 0.005 0.007 0.015 0.025 0.034 0.049 0,074 0.091 3/4 0.102 0.280 0.390 0.710 1.300 1.820 2.600 3.900 5.200 1.0 0,039 ~-"- J,aa, 0.2 7 0.All5 0,693 1,000 1,183 1.1180

4.0 1•1/4 0.013 ~.o33 .051 0.0 9 0.185 u.n, 0.330 OA95 0.880 1-1/2 o.uu, M18 l,02 0,u 0,0811 0.125 0.178 0.287 0.358 2,0 o.003 ~.007 .011 11,0 0 11,033 11,1148 11.1118 o.098 11,131 3/4 0.127 0.324 UH 0,97S 1.825 2.275 3.250 4.870 8.490 1.0 0,048 0.124 0.116 0.371 0.819 0.888 1.237 1.854 2.470

5.0 1-1/4 0,018 0.041 0.082 0,124 0,207 0.289 0.413 0.819 0.825 1-1/2 0.009 0.022 0.033 0.087 0,111 0.158 0.223 0,334 0.446 2.0 0.003 0.001 0.012 0.025 0.041 0.057 0.082 0.123 0.184 1.0 0,073 0.188 0.271 0.557 0.928 1.299 UH 2.780 3.710

M/4 0.024 0.082 0.093 0.118 0.310 0.443 0.820 0.921 1,231 7.5 1-1/2 0.013 0,033 0.050 0.100 0.187 0.234 0,334 0.500 0.881

2.0 0.005 0.012 0.018 0.037 0.082 o.oae 0.123 0.114 0.248 2-1/2 0.002 0.008 0.009 0.01' 0.030 0.042 0.080 0.091 0.121 1.0 0.097 0.247 0.371 0.742 1.237 1.732 2.475 3.710 4.1M5

1-1/4 0.032 0.083 0.124 0.241 0.413 0.578 1.858 2.480 3.310 10.0 1-1/2 0,018 0.045 0.087 0,134 0,223 0.312 0.448 o.eea 0,891

2.0 11.008 11,018 0.025 o.-- 11,unL 11.,n 0,114 0~48 0,328 2.1,2 0,003 0,008 0.012 o.024 0,040 0,088 o.uo 0,121 0,181 1.0 0121 0.309 0.A84 0.928 1,547 2.165 3,093 4.830 8,110

1•1/4 0.040 0.103 0.155 0.310 0.518 0.723 1.033 1.547 2.083 12.5 M/2 0.022 0.058 0.014 0.187 0.279 0.390 0.557 0.835 1.114

2.0 0.008 0.20 0.031 0,082 0.103 0.144 0.205 0.307 0.410 2-1/2 0.004 0.010 0.015 0.030 0.050 0.071 0.101 0.151 0.201 1-114 0.048 0.124 0.186 0.372 0.820 0.887 1.239 1.857 1.478 1·1/2 0.028 0.097 0.100 0.200 0.334 OA68 0.889 1.002 1,337

15.0 2.0 0.009 0.025 0.037 0.074 0.123 0.172 0,248 0.389 0.492 2-1/2 0.005 0.012 0.018 0.038 0,080 0.015 0.121 0.180 0,242 3.0 0.002 0.005 O,uun 0.1115 11,uLn O,uan 0,UO O.u,u 0.101

1-114 0.057 0.145 0.217 0.433 0.723 1.012 1.44. 2.1H 2.889 1-112 0.031 0.078 0.117 0.234 0.390 0.548 0.780 1.170 1.580

17.5 2.0 0,011 0.029 0.043 0.088 0.144 0.201 0.287 O.A30 0.574 2-1,2 0.008 0.014 0.021 0.042 0.071 0.099 0.141 0.211 0.282

J,U u. u. o., .... 0,U'lG O,uau 0,114 O,u,w O,uftw 0.11, 1-114 0.065 0.185 0.241 0.498 0.128 1.157 1.852 2.475 3.300 M/2 0.035 0.089 0.134 0.281 0.448 0,824 0.892 1.338 1.782

20.0 2.0 0,013 0,033 0.049 0.098 0.104 0.230 0.328 0,192 0.856 2-1/2 0.007 0.018 0.025 0.048 0.081 0.113 0.181 0,242 0,322 3.0 0.003 0.007 0.010 0.020 0.034 0.047 0.088 0.101 0.135

NOTE I For liquids with a specific gravity (s.g.) other than 1.0 (water= 1.0) multiply the above friction loss values by the s.g. of the liquid.

...

("

TYPE OF FITTING OR VALVE (1)

PIPE I SIZE GATE GLOBE CHECK ELL (2) ELL TEE TEE (2) NPS VALVE VALVE VALVE STANDARD STANDARD SGT. THRU RGT. ANGLE

(OPEN) (OPEN) (OPEN) 90° 45° FLOW FLOW

1,2 I 0.35 17 4.0 1.5 0.8 1.0 3.2

3/4 0.50 22 5.5 2.2 1.0 1.3 4.5

0.60 27 6.0 2.7 1.3 1.7 5.7

1-1/4 0.80 38 9.0 3.6 1.7 2.3 7.5

1-1/2 1.20 44 11.0 4.5 2.0 2.8 9.0

2 1.20 53 14.0 5.2 2.6 3.5 12.0

2-1/2 1.40 68 17.0 6.5 3.0 4.3 14.0

3 1.70 80 20.0 8.0 4.0 5.2 16.0

4 2.30 120 25.0 11.0 5.0 7.0 22.0

5 2.80 140 34.0 14.0 6.2 9.0 27.0

6 3.50 170 40.0 16.0 7.8 11.0 33.0

8 4.50 220 54.0 21.0 11.0 14.0 43.0

10 5.70 280 67.0 26.0 14.0 17.0 53.0 I

I NOTES I (1) PREFERRED ANTI-SIPHON VALVES REQUIRE A MINIMUM OF 2" HG TO OPERATE.

(2) BASKET TYPE STRAINERS THAT ARE LINE SIZE HAVE A FRICTION LOSS SIMILAR TO A 90" ELL. STRAINERS ONE LINE SIZE SMALLER ARE SIMILAR TO A RIGHT ANGLE TEE.

VISCOSITY VELOCITY IN FT./SEC. VISCOSITY VELOCITY IN FT./SEC.

ssu cs SUCTION DISCHARGE ssu cs SUCTION DISCHARGE

40 3.9 5.0 10.0 1500 330 2.5 4.3 100 19.5 4.7 8.0 2500 550 1.6 2.7 200 43 4.4 7.3 5000 1100 .85 1.5

400 88 4.0 6.8 7500 1650 .50 .85

750 165 3.3 5.6 10,000 2198 .30 .50

r

r

r \,

0

m D C

~ ~ r m z -i c., Cl) 0

C 0 .... -i 0

0"' z 0

C z m r m z -Ci) 0 -i 0

::c I

-n m m -f N

0 0

c., 0 0

81

LIFT-FEET

0"' 0 _.!=) !=' !=> OI <..> .a,. (JI 0

CAPACITY - GPM

N 0 "' 0 .... "' 0 C)

0 0

"' 0 0

I I

rm • • I I - J -I ii " -I - J,,f -I ~ ,- • ' I l-1-W J J d --+-+ • ; ~ - .! ,lJ, -

-~ ittH .. : it ,- • 7 • ,, I ,, I, .. ,, ' ' ~~ ' ' ' • ' l ~ . I, ' , !l~ • ' ' ' ' • f'

' • ' en• r ' ' ' , ' " ' ' ' ~1~· I ' d. ' ' q, /. . . . . ' : I

I f:0

0 j 1

• 1 •

2~-• C I ' I , L • ' ' r '

1

·~·-r11 IU1-' ~ r ~ Wlll1111r'l..1 •~, ~,, , I .... I Q2!' ,, I ',,_V-, ..... I I.,_

n ill:'!i , , , i • i -i'I"""""""." ' • , ' II, "lllJfl~I l-itJ~ti.1-.:~ l'Ht ::o- , -;. , ~ . f- H--t-77 IJLL-+ .,-- , • ~, -~, '. n J -fit.1nx 11 1

1

• 1 11

, ... .,_ , • " I' ' ...... , --,f--l-- , , ' ' I,'' ' ' ,_ • r, '.

fllt.,._Jrl' I ,-tt•I O ' ' • ~ , 1 ~ r r"'li,,,, ,,, 1-J r

p ', " " h' • " t'_ '" I- . , n, ' 1 I ::_ ' j J I ,_ ' , : " ~ ' ~ , ~TI f...jl rx.1 Ii I j , '

1

"j

IIUI -I t-> I • ., i ~ I I • I • ~ ~ ~ ~ .._

-11111 ; ... ' r' ' ' µ, ' ' '' ' -1111 -1 r-. .. , ; ;.; ; L, • ' _ - - -LJ JJ L...IJJJ

1.98 2.65 3.97 5.29 6.61 13.22 318" ._.,_ __ ._ ____ ..L ____ ___,314• L---L-....L---L-----.1---.J

1.32 1.75 2.19 4.39 8.77 2.2 2.65 3.53 4.41 8.82 13.22 1/2" -------------~---- 1· .___...._ ___ _

1.56 2.22 4.44 6.67 8.89 11.1 2.83 4.72

VELOCITY - FEET PER SECOND

LIFT-FEET CAPACITY • GPM

0

m D C < ~ )> r m z c., -i 0

Cl) C ..,. 0 0

-i 0 g z r z m r m z g Ci) -i ::c I

-n m m -i ~

0

8

0"' 0 -!=> "'"'

2.19 318"

1.26

0

4.39

2.53 1/2"

1.47

6.58

N 0

5.05

2.95 511"

1.95

"' 0

2.21

7.58

4.42

2.89

.... u, b b

2.95 3.69 1·

2.48

5.90 7 .37 8.85

3.85 4.82

0 0

7.37

4.13 1-1/4"

2.64

9.63

VELOCITY - FEET PER SECOND

11.06

N 0 0

8.25

5.27

"' 0 0

12.38

.... 0 0

0 ::r CJ ::i. N

(")

0 "C "C m

z :;o 0~ ·c NOJ Oz r= c,

I (/) ~­c~ Cl>Z (/) C) Cn

I :c ~)> CD :::0 (") ~ (/) I

~ -< "C m

"

m D C

0

~ ~ r m z -f :::: en C 0 ... -f 0

0"' z 0

r z m r m z -Ci) 8

:i! •

"11 m m -f "'

8

"' 8

61

LIFT-FEET CAPACITY • GPM

0 "' 0

0

m D C

~ ~ r m z --t ~ en C 0 .. --t 0

0 g: z r z m r m z -Ci) 8 --t :I: . "11 m m --t "'

0 0

w 0 0

LIFT-FEET 0"' 0 "'-

~

~"' l""O

~ ... I""'-

~~ ....

"" ~ ~ -~ ~" 1, /

~"' ""111o.. , ...... ...

... ~

~"" ...... "- / ,,

~"" ~~

"' 1/2" NPS 1.05

314" NPS 0.60

"' w ... "'

1.68 3.37 5.05 6.73 8.42 2.23

0

3.71

"' 0

7.42

w 0

11.14 1/2" NPS I 1-1/4" NPS

1 I 1.58 2.11 3.16 4.22 5.27 10.55 2.57 4.29

6.44. 314" NPS 2.41 3.0 6.02 12.03

VELOCITY· FEET PER SECOND

CAPACITY • GPM 0

.., w ... "' "' c., ... "' 0 0 0 0

/ ~' .Y i,i ~~ ,J

~ ,

~

I/ / ~

~ , ./

-l II,, / :+-* ~v I b'B

~ ~' / I~

,J ~ / ,) , r,j:, 1 ~ j

1./ ./ ,J

~v ~ / ~ ~,, .~;, ~ -~ ,. &'B V .. C ,J ~ .. ./ ,, ./ ,, I ~ 0► Z-4

~' I ~..:" V en :!j::c"'

~~ ,, ,,_F* ./

• ~:-0 oc:,G>

~ ::I• jlll , ~ / ,y" u,0 •

~ ~ .ll z~~ . --., ,, ,, ::c.., c;,.,.

I/ V / ..,c:: ~ ~

!D~

I / V ;!I -1-1/2" NPS .

2.11 3.16 422 5.27 1.58 3.15 4.73

1.20 1.80 2.41 3.00 6.~2 12.03 1"NPS

0.74 1.11 1.48 1.86 3.71 7.42 11.14 1-1H"NPS -1.29 2.15 4.29 6.44

VELOCITY· FEET PER SECOND

,

:,

~

?

r

r

C

Ol

LIFT-FEET CAPACITY - GPM 0"' 0 "' 0 l:l ::: ..

0 g; "' g g

0 ln .. l, , 1 1 I I I I I I I,, I I> I I :al I • I :al

~

c. "'" ;;:o _, II Ill IA 111, ► I I I VI I I • r w1 I II I J<a II , 11 I !l] • Ill" II II I II II • - I I "'I I II II .,. II II '" I -I ,~, .. 1111:.. en -IIIM-1tt;--r, I V I I I I -

~ : IJW I IV I I I I I A I I I I I I ~;-~ I I z r-z m r-~ 8 1111111\1\MI 1 ~ :c

• I I I I I I I I I I I "II ...- I I I Y I m I., I I IA 11 I I I 1 .. m I" 11 I I • -1 8 1111111\1 Is..

c.> 11111 I 11 I a I 8 3/4"NPS

11 I LI I W: I I I I I « I I I I I 5 I

.73 .96 1.91 2.87 3.82 4.78 9.56 t"NPS ._ ____ __._ __ _.. __ .__. _____ ...___, ._ __ ._ __ ...._ _ _.__...__2-1/2" NPS,_.._ ____ _.

.37 1-1/4" NPS

LIFT-FEET 0 (.h 0

.74 1.11 1.48 1.86 3.71 4.64 .87 1.34 2.00 2.68 3.35 6.7

.28 .43 .64 .86 1.07 2.15 4.29 6.« 8.58 t-t/2"NPS

.39 .47 .63 .79 1.58 3.15 4.73 6.30 7.88 11.8

VELOCITY - FEET PER SECOND

..... CAPACITY - GPM 0

.., 0 ::: t; g; 0

0 l:l 0

o •ml , , , , I I I I :al I I » I· , > , I I I » I - I I

m D C

j; • _, I I I A I I I I I VI I I I I I I I;; ~'f I I I I. L.J I I I I I • ~ l!l 111111..111 I I I Y I I I I I •

co 'I ll".J<l 11111 , I g t; l]tj] I I ' I I I I.- ., .-·1 I I I I.A I I I I I I ~ I I 5 ~ N ~ I I I ,: I I I :A I I I I I I:>. I I I z r-z

m • 1 I I I I I I. I;; I I HF I I I l>'f' I I I I I> ~ g 1111111'.N" 11 I I >'f' I I • -I :J:

;, Ill 11111 I I:; • I l4f I I I I I I/ I I I I I I :A -I g 1111111'.I I P...11 I I I Lr I I •

~ 111111 11 I 9 I I I « I I I I II I I I I I I < I I I I I I I I I I I ! I 0 I L 2-1/2"NPS _._ _____ ._ ____ - ______ _

.34 .67 1.34 2.00 2.68 3.35 6.03 1-1/4" NPS .._ ____ ....__ __ ....___.....__.._ __ __, l._3"NPS--'--_._ _ _.__..._ ___ __...__ ___ __.

t-1/2"NPS

.21

.16 TNPS

.43

.32

.14 .19

.64 .86 1.07 1.61 .43 .87 1.30 1.74 2. 17 4.34 .__,..__...__..__,.NPs-...._ ____ _.

.47 .63 .79 1.58 2.36 .55 .76 1.00 1.26 2.52

.29 .38 .48 .96 1.91 2.87 4.30

VELOCITY - FEET PER SECOND

m D C

0

< ~ )> r m z"' -i 0

{/J

C • 0 0

-i 0 g z r z m r m z -Ci) 8 -i :::c I

-n m m -i g

8

IZ

LIFT-FEET CAPACITY - GPM 0"' 0 "'- N <-> .. "' 0 N

0 "' 0 .. 0 g: g

..... ;1

1

' ~ I\

' \ m111 \

\. 1

\

'' ' !\ \ 1 '

\

' ' , 1-1~"NPS

1-1/2" NPS

2"NPS

El I lkff lJJEf 11 lml I !mII I 111111. I I y I I I ¥ I I I I I IA I r I I I fsf I. I I I I I I I I I I I~

I ~ I I I ff I I I I I 1' I I I I I I VI I t I I I I I I I I I .~-~

4"NPS .20 .40 .so .76 1.00 1.26 2.52

.16 .32 .47 .63 .79 1.58

.01 .19 .29 .38 .48 .96 1.91 2.87 2-1/2" NPS I

.15 .20 27 .34 .67 1.34 2.00 2.68 3.35 4.00 3" NPS

22 .43 .87 1.30 1.74 2.17 4.34

VELOCITY - FEET PER SECOND

8 ~

') S.86

~

BACK PRESSURE REGULATOR VALVE Back pressure regulator valves are not supplied as stan­dard on John Zink pump sets. When required, order sep­arately to be shipped loose.

Flow chart is for Cash-Acme Model FRIO with viton non-metallic diaphragm and a 100/4 rise in pressure from set point flowing No. 2 oil ( eg. A valve flowing the full discharge capacity of a pump will have a 10% rise in pressure from set point. For a more sensitive pressure control, select the valve with next pipe size larger. For a less sensitive pressure control, use the capacities listed in the 20% or 30% pressure rise column.)

SIZE RANGE OF ADJUSTMENT IN PSI

(inches)

1/2 0-25 5-50 30-100 75-175 100-250

·3/4 0-10 10-50 20-110 30-150 100-250

1 0-20 20-90 40-125 50-250 - -

1-1/4 0-15 20-85 40-125 50-250 - -

1-1/2, 2 0-10 10-55 30-100 40-200 125-250

VISCOSITY CORRECTION FOR VALVE SIZING Fluids such as No. 4, 5 & 6 oil can be quite viscous and an adjustment must be made to properly size valves for these applications.

VISCOSITY CORRECTION FACTOR

VISCOSITYfTEMPERATURE IN SSU CORR. ssu FUEL GRADE TEMP. °F FACTOR

100 #4 70° F .78 200 #5 Light 100° F .71 500 #5 Heavy 100° F .62

1000 #6 Lower limit 100° F .56 2000 #6 Upper limit 130° F .52

The above chart is for ref. points on the viscosity-tem­perature chart for No. 2-4-5 and 6 fuel oils.

Example of Sizing for Viscous Liquids. What size valve is required to pass 5 GPM of heavy oil, viscosity of 750 SSU at flowing temperature.

Answer: 5 GPM -:- factor .59 (by interpolation) = 8.5 GPM of equivalent flow.

Size the valve at the 8.5 GPM (100/o column) level and at the operating pressure.

BACK PRESSURE REGULATOR FLOW CHART No. 2 oil Cash-Acme Model FR10

~ a.. (!)

0

p

118: 66· 25 -

77 - 54

66: 44- 20 60 40

50 32 - - 15

46 27

34- 20- 10 30 18 27 16 23 15 20 13 18- 11- 5 14 8 4

8 6 3

6 4 2

3 - 2 1

IJOO!c 20% 10% RESSURE RISE

IN%

"' ...... --~--... --.... . ..

10

0

with non-metallic diaphragm

--~ --- - -, - fl' I~ -- ,..

~ , ~ .... "' r~ -.~(?--' ,~ ....... ,,.,, ,,'l- 'i~~ ~ .. ...... ~/'~ -~~ fl'

~ IIO (\b. .,. ~ lo i., \' I )':J .,..

~ .~(?

-_,

.,..!\

--~ ~ -.. "' -~ -- ,,, ..... ~, a:"'~~ - -- -lo ~ .-

...... -- --~. I -•• • ,rt "'~;;r ...

•• ~

.....

20 30 40 50 100 20 0 PRESSURE - PSI (Spring Set Point)

22

'

J

~

C

.. iii -O>::f co a, 8~::> a, a, CCI)

Cl)C/)::)CI)

••32

•'"35

----45

•io■ 50

- 60 • •70 • •80

- •90 • -1-

••200

••300

.,.400 •io■ 500

•io■ 600

•'"700 .,.eoo • '° 1,000

• io■ 2,000

• '"3,000

• 1■ 4,000

• io■ S,000

• io■ S,000

• •7,000

• -a.

• 18

• •20

30

=

- 50

••60 ••70 =-~ --100

••200

••300

•1■ 400

·•500 •io■ 600

•'"700

• •10,000 • "'1,000

• •20,000 • "'2.000

• •30,000 • •3,000

• •40;000 • •4,000

• '"50,000 • •5,000 • •60,000 • •s.OOQ

- '"811.000 - •B,000

- --100,000• • 10,000

• •200,000• • 20,000

VISCOSITY CONVERSION CHART

.

. - 30

~.,

4 • • 35

- ·-" u

••so 10

•io■ 60

•io■ 70

... 80 20-- i,,-90

... 100

JU

• • 15

"" ""' 200 - ?I\

50

60 2-

... 300 - 30 ~eo ·-100~ --400

""500 • - 50

• - 600 • • 60 • - 700 • • 70

200 ~ --•• 900 •• 90 • • 1,000 " • 100

300

~400

~ 500---" --2.000-. -2:::::

~600

••3000 -- 300 ~ 800

.1, ___ 4,000 •-400

"• 5,000 -- 500 • • 6,000 -- 600 • • 7,000 •• 700

, . ., ........ - u.--- - "'900 -• 9,000 • ""1,000 10,000 -.~

.. -g. 8a •c Cl)W

::>4

• - 56

• - 60

7-

-... 80

- .. <Ill

... 100

-- 200

""' 300

•= • - 600

700 • - 800 • - 900

.. a, ... a, a, O>o •c ow

1.u

1.1

... 12

... 1.4

-- 1."

L

-"' 2

---- 4

... 5

""' 6 ""' 7

0

••9 1-

• • 1,000 " - 20

• - 30

2,000--. ..-4u

..... ■ • 3,000 •

- 60 • • 70 .

= • • 5,000 :

• 90 1""

7,000

• • 10,000 • - 200

• - 300

20;000-.. ..-4UU

-- 500 4.~ ~.ooo • • 30,000. - ... ?n,000~ - 600 5,---

"· ·-- ~o.

., Q. "'Cl::, cO 8-e~ a, O 0 OOLLZ

·-

... 50

""' 75

""' 100

•"' 150

---~400

• ""500

• I■ 700

• • 1,000

- 1,200 ■ • 1,500

• • 1,700

... 5

·"' 6 • 115

-- 25 ... 7

-- 8 - 50 •• 9

... 50 •• 10

• • 25

""' 75 1-·-""' 100 1"

1·- -- 25 1-

·-

-• "" 300 • - 5

• I■ 400 -- 75 • 4.3 - ... 100 • 3.75

• • 700 • • 3.3

·- 15()---;; •2.4

1--

• - 1,200 - .. 200 -- 1.5

.... .. . "'Cl 0

8f~ a, "' ::, Cl)Q.0

•• 20

... 25

JU

""' 35

•• 40

""' 45

--

75

""' 100

... 200

... 300

0 .. . "'Cl 0 CcZ 8=t: a. a, "' ::, Cl)Q.0

-- 25

-- 50

1uu

-- 200

-- 300

-- 500

... 750

... 950

v.-- ... =,OOQ..! ~3.000 • • 50,000- • 1,000_ CONVERSION FACTORS ... 60,000

10, ___ ' - ,000-., -4, -"' 70,000 Centipoises

Centistokes = •"' 50,000 • • 5,000 Specific Gravity •"' 60,000 • • '6;Il00 • io■ 100:000, "'2,000

-80,()()()-4, -a . SSU* = Centistokes x 4.55 ... ,000--

• • ·100,00IJ'. • ,10,000 • • 3,000

Degrees Engler* = Centistokes x .132

It) ... .. . "'Cl 0

8f~ . "' ::, Cl)Q.0

•5.0

• •5.5

0 N ., .

"'Cl 0 sf~ a, Ill ::, Cl)Q.0

2.5

. -3.0

:.o--.. • •6.5

• •7.0 -_5-

. -■ .10

.. • • 15 ... - 20

• •JO

- 40 ... . ""

•"'60 . "' nft

• • 100 ... ■ • 150

... • •200 . -

3.5

4.0

4.5

5.0

7.5

10

15

20

25

30

40

50

70

30, -~.000. -4,000- Seconds Redwood IO = Centistokes x 4.05 40,_ :_

5,000_ *Where Centistokes are greater than 50

•.., =n,000: ~.000 " • 300,000, • 6 000 50 • . . ,vuu

VIKING PUMP, INC. • A Unit of IDEX Corporation • Cedar Falls, Iowa 50613 U.S.A.

23

N .i::.

50,000

20,000

10,000

5,000

4,000

Cl) 3,000

C Z 2,000 0 U 1,500 w en ..J 1,000

< 750 en 0:: w > 500 z

400 ::> ~ 300 0 al

~ 200 en

~ en

150

0 u en > 100

90

80

70

60

55

50 0 10 20 30 40 50 80 70 80 90 100 110 120 130 140 H50 180 170 180 190 200 210 220 230 240 250 280 270 280 290 300 310 320 330

TEMPERATURE, DEGREES FAHRENHEIT

Determining pumping and atomizing temperatures for fuel oils - The chart indicates limits of viscosity recommended in each grade by the U.S. Bureau of Standards. Viscosities between 2000 and 5000 SSU is considered to be easy pumping and viscosities between 5000 and 10,000 SSU are considered to be pumpable. Viscosities above 10,000 SSU, depending on pump speed, may be too viscous to flow.

On the chart the upper limit of No. 6 oil as a standard intersects at approximately the I 0,000 SSU

'-' \.,I

and the I 00° F line and requires a temperature of 230° to 255° F for the atomizing range.

Source of the crude oil detennines the slope of the line. For example: Residual oil from Pennsylvania crude can have a viscosity of 1050 SSU at 140° F and 240 SSU at 210° F. This is plotted on the Chart. Viscosities at two different temperatures are required to properly chart the slope of the line. Research the source to know the characteristics of the oil being delivered.

'-'