api piping plan
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API ENVIRONMENTAL PIPING PLAN
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- REVIEW
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RequirementsRequirements of Gas Sealsof Gas Seals
Gas or vapor suitable for sealing{Availability,Safety & Environmental concern}
Constant & reliable supply of external
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Buffer/barrier gas free from contaminationfrom both liquids and solids
Process fluids which are not adversely
affected by barrier gas leakage
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PurposePurpose of Piping Plansof Piping Plans
Flushing to remove heat
Lowering fluid temperature
Create a more favorable environment for themechanical seal
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Altering the seal chamber pressure
Cleaning the process fluids
Control atmospheric side of seal
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PurposePurpose of Piping Plansof Piping Plans
Capture and/or prevent leakage
Provide a means of detecting and controlling seal
leakage
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e ec ea ageRoute leakage to appropriate collection or
disposal system
Provide fluid other than process fluid for theseal environment
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Methods of Achieving GoalsMethods of Achieving Goals
Piping or routing of process fluids
Introduction of external fluids
Auxiliary equipment
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Seal coolersCyclone separators
Reservoirs
Instrumentation
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Piping PlansPiping Plans Standardized in:
API 610 API 682
ISO 21049
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ASME B73
Designated by numbers
API example 11, 32, or 53
ASME example 7311, 7332, or 7353
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Plan 01Plan 01
What Internal seal chamber flush
from pump discharge.
Operates similar to Plan 11
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Plan 01Plan 01Why
Seal chamber heat removal. Seal chamber venting on
horizontal pumps.
Reduce risk of freezing orol merizin fluid in ex osed
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Plan 11 piping.
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Plan 01Plan 01
Where Custom seal chamber, most
likely an ASME/ANSI pump.
Clean, moderate
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.
Used with single seals,rarely used with dual seals.
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Plan 01Plan 01
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Flush typically can not bedirected over the seal facesand heat removal is limited.
Calculate flush flow rate based
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on head loss through internalporting.
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Plan 02Plan 02
What Dead-ended seal
chamber with no flush.
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Plan 02Plan 02
Why Simplicity no environmental
controls.
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Plan 02Plan 02Where
Large bore or open throat sealchambers in moderatetemperature services.
Clean fluids.
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op-entry m xers or ag tatorswith dry seals.
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Plan 02Plan 02Preventative Maintenance
Process must have adequateboiling point margin to avoidvaporization.
Cooling fluid in seal chamber
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in hot services.
Often used in combination with
steam quench, Plan 62.
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Plan 11Plan 11
What Seal flush from pump
discharge through orifice.
Default sin le seal flush
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plan.
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CentrifugalCentrifugal PumpPump
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Plan 11Plan 11
Why Seal chamber heat
removal. Seal chamber venting on
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z u . Increase seal chamber
pressure and fluid vapormargin.
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Plan 11Plan 11
Where General applications with
clean fluids.
Non- ol merizin fluids.
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Plan 11Plan 11Preventative Maintenance Use an orifice with a minimum
0.125 (3 mm) diameter. Calculate flow rates to size
orifice for adequate sealchamber flow.
Increase boilin oint mar in
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with proper orifice and throatbushing sizing. Flush should be directed over
seal faces with piping at 12Oclock position.
Typical failure mode is aclogged orifice checktemperatures at pipe ends.
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ErosionErosion
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Plan 13Plan 13
What Recirculation from seal
chamber to pump suctionthrough orifice.
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Standard flush plan onvertical pumps.
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Plan 13Plan 13
Why Continuous seal chamber
venting on vertical pumps.
Seal chamber heat removal.
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Plan 13Plan 13
Where Vertical pumps.
Seal chamber pressure isgreater than suction pressure.
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with moderate solids. Non-polymerizing fluids.
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Plan 13Plan 13Preventative Maintenance
Vent piping loop prior to startingvertical pumps. Use an orifice with a minimum
0.125 (3 mm) diameter. Calculate flow rates to size orifice
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for adequate seal chamber flow.
Reduce seal chamber pressurewith proper orifice and throatbushing sizing.
Typical failure mode is a cloggedorifice check temperature at pipe
ends.
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Plan 14Plan 14
What Seal flush from pump
discharge andrecirculation to pump
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suction with orifices. Combination of Plan 11
and Plan 13.
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Plan 14Plan 14
Why
Continuous seal chamberventing on vertical pumps.
Seal chamber heat removal.
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pressure and fluid vapormargin.
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Plan 14Plan 14
Where
Vertical seal.
Clean, non-polymerizing fluidsat moderate temperatures.
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Plan 14Plan 14Preventative Maintenance Use an orifice with a minimum
0.125 (3 mm) diameter.
Calculate flow rates to size orificefor adequate seal chamber flow.
Increase boiling point margin withproper orifice and throat bushing
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sizing.
Flush should be directed over sealfaces.
Vent piping loop prior to startingvertical pumps.
Typical failure mode is a clogged
orifice check temperatures atpipe ends.
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Plan 21Plan 21
What
Seal flush from pumpdischarge through orifice andcooler.
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increases heat removal.
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Plan 21Plan 21
Why
Seal cooling. Reduce fluid temperature to
increase fluid vapor margin.
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.
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Plan 21Plan 21
Where
High temperature service,typically less than 350 F (177C).
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.
Clean, non-polymerizing fluids.
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Plan 21Plan 21Preventative Maintenance
Seal cooler and piping must haveair vents at highest elevation vent before starting.
When using 682 Seal Cooler, pipe
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transfer. Use an orifice with a minimum
0.125 (3 mm) diameter.
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Plan 21Plan 21Preventative Maintenance
(continued) Calculate flow rates to size orificefor adequate seal chamber flow.
Increase boiling point margin withro er orifice and throat bushin
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sizing.
Regularly monitor device inlet andoutlet temperatures for signs ofclogging or fouling.
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Plan 23Plan 23
What Seal flush from internal
pumping device throughcooler.
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Standard flush plan in hotwater services.
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Plan 23Plan 23
Why Efficient seal cooling with
low cooler duty.
Increase va or mar in.
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Improve water lubricity.
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Plan 23Plan 23
Where
High temperature service, hothydrocarbons.
Boiler feed water and hot water
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.
Clean, non-polymerizing fluids.
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Plan 23Plan 23
Preventative Maintenance
Seal cooler piping must haveair vents at highest elevation vent before starting.
When usin 682 Seal Cooler
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pipe with parallel flow tominimize head loss.
Seal chamber requires closeclearance throat bushing toisolate process fluid.
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Plan 23Plan 23
Preventative Maintenance
(continued) Tangential seal gland taps
should enter at bottom and exitat to .
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Regularly monitor cooler inletand outlet temperatures forsigns of plugging or fouling.
Process fluids with iron shouldflow through magneticseparator before cooler.
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Plan 31Plan 31
What Seal flush from pump
discharge throughcyclone separator.
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Centrifuged solids arereturned to pump suction.
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Plan 31Plan 31
Why
Seal chamber heat removal. Solids removal from flush and
seal chamber
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Plan 31Plan 31
Where
Dirty or contaminated fluids,water with sand or pipe slag.
Non-polymerizing fluids.
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Plan 31Plan 31Preventative Maintenance Cyclone separator works best on
solids with a specific gravity twicethe process fluid.
Seal chamber pressure must benearly equal to suction pressure
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or proper ows.
Piping should not include anorifice and is not expected to ventthe seal chamber.
Typical failure mode is a cloggedseparator or pipes checktemperatures at pipe ends.
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Fluid Entry from
Pump Discharge
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Clean Light FluidDischarge from
Separator to SealChamber
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Fluid Entry from
Pump Discharge
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Clean Light FluidDischarge from
Separator to SealChamber
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Fluid Entry from
Pump DischargeHeavy Dirty FluidDischarge fromSeparator Back
to Pump Suction
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Plan 32Plan 32
Why
Seal chamber heat removal. Process and solids removal
from seal chamber.
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pressure and fluid vapormargin.
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Plan 32Plan 32
What
Seal flush from an externalclean source.
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Plan 32Plan 32
Where
Dirty or contaminated fluids,paper pulp.
High temperature service.
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fluids.
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Plan 32Plan 32Preventative Maintenance Use throat bushing sized to hold
pressure or maintain flow velocity. To restrict dirty process fluid,
regulate injection flow rate. To increase fluid va or mar in
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regulate injection pressure.
Injection fluid must be compatiblewith process fluid.
Regularly monitor controlsystem for closed valves orsigns of plugging.
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Plan 41Plan 41
What
Seal flush from pumpdischarge through cycloneseparator and cooler.
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Plan 31.
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Plan 41Plan 41
Why
Seal cooling. Solids removal from flush and
seal chamber.
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Plan 41Plan 41Where
High temperature service,typically less than 350 F (177C).
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,
water with sand or pipe slag. Non-polymerizing fluids.
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Plan 41Plan 41Preventative Maintenance Seal cooler piping must have air
vents at highest elevation ventbefore starting.
When using 682 Seal Cooler, pipewith series flow to maximize heat
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transfer.
Cyclone separator works best onsolids with a specific gravity twicethe process fluid.
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Plan 41Plan 41Preventative Maintenance
(continued) Seal chamber pressure must
be nearly equal to suctionressure for ro er flows.
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Typical failure mode is cloggedseparator or pipes checktemperatures at pipe ends.
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Standard Flush Plans
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Standard Flush Plans
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Seal Chamber for Plan 51
Key
1 ReservoirV Vent (if required)
Q QuenchD Drain (Plugged)F Flush
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Combination Flush Plans
Sin le Seal Arran ements
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Plan 31
Plan 21
Standard Flush Plans
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API Plan 41
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Standard Flush Plans
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API Plan 11 / ANSI Plan 7311: Recirculation
from pump discharge through a flow controlorifice (if specified) to the seal.
API 62 / ANSI 7362:
Exterior source providing aquench.
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Standard Flush Plans
Plan 11
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Plan 11
Standard Flush Plans
Steam
3-5 PSI
Plan 62
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Steam Out
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Plan 52Plan 52Why
Outboard seal acts as asafety backup to the primaryseal.
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emissions.
No process contamination isallowed.
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Plan 52Plan 52What
Unpressurized buffer fluidcirculation through reservoir.
Fluid is circulated by a
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seal assembly.
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Plan 52Plan 52Where
Used with dualunpressurized seals(tandem).
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,light hydrocarbons.
Hazardous or toxic fluids.
Heat transfer fluids.
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Plan 52Plan 52Preventative Maintenance Piping loop must self-vent to
vapor recovery/flare systemnear atmospheric pressure. Process vapor pressure is
generally greater than reservoir
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. Buffer fluid must be compatible
with process leakage.Reservoir level gage indicatesoutboard seal leakage.
Primary seal leakage isindicated by increased ventpressure.
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Plan 53APlan 53AWhat
Pressurized barrierfluid circulationthrough reservoir.
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Fluid is circulated bya pumping ring inthe dual seal
assembly.
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Plan 53APlan 53AWhy
Isolate processfluids.
Z r r
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emissions.
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Plan 53APlan 53AWhere
Used with dual pressurized
seals (double). High vapor pressure fluids,light hydrocarbons.
Hazardous or toxic fluids.
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Heat transfer fluids.
Dirty, abrasive orpolymerizing fluids.
Mixers or agitators.
Vacuum service.
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Plan 53APlan 53APreventative Maintenance
Piping loop must self-vent to
reservoir located at highestelevation.
Pressurize reservoir at alltimes, maximum gas charge
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150 - 200 psi (10 - 14 bar)
Barrier fluid must becompatible with process.
Reservoir level gageindicates both IB and OBseal leakage.
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Plan 53BPlan 53BWhat
Pressurized barrierfluid circulation witha bladder
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accumulator.
Fluid is circulated bya pumping ring inthe dual sealassembly.
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Plan 53BPlan 53BWhy
Isolate process fluid. Zero process
mi i n .
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Higher pressurethan Plan 53A.
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Plan 53BPlan 53BPreventative Maintenance
Piping loop must be fully
vented before starting. Accumulator must bepressurized at all times,usually by gas charge.
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Barrier fluid must be
compatible with process. Regularly monitor barrier
pressure manually addbarrier fluid when pressuredecays.
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Plan 53CPlan 53CWhat
Pressurized barrierfluid circulation witha piston
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accumulator.
Fluid is circulated bya pumping ring inthe dual sealassembly.
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Plan 53CPlan 53CWhy
Isolate process fluid. Zero process
mi i n .
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Higher pressurethan Plan 53A.
Dynamic tracking of
system pressure.
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Plan 53CPlan 53CWhere
Used with dual
pressurized seals(double).
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fluids, lighthydrocarbons.
Hazardous or toxicfluids.
Heat transfer fluids.
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Plan 53CPlan 53CPreventative Maintenance
Piping loop must be fullyvented before starting.
Reference line must tolerateprocess contaminationwithout plugging.
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Barrier fluid must be
compatible with process. Reservoir level gage
indicates both inboard andoutboard seal leakage.
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Plan 54Plan 54What
Pressurized barrierfluid circulation byan external system.
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Plan 54Plan 54Why
Isolate process fluid. Zero process
mi i n .
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Seal cannot inducecirculation.
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Plan 54Plan 54Where
Used with dual pressurizedseals (double).
High vapor pressure fluids,light hydrocarbons.
Hazardous or toxic fluids.
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Heat transfer fluids.
Dirty, abrasive, orpolymerizing fluids.
Mixers or agitators.
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Plan 54Plan 54Preventative Maintenance
Piping loop must be fullyvented before starting.
Circulating system must bepressurized and energized atall times.
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Barrier fluid must be
compatible with process. Circulation system level
gage indicates both inboardand outboard seal leakage.
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Plan 62Plan 62What
External quench onatmospheric side ofseal.
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Quench fluidstypically steam,nitrogen, or water.
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Plan 62Plan 62Why
Prevent solidsbuildup onatmospheric side of
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seal.
Prevent icing.
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Plan 62Plan 62Where
Used with single seals.
Oxidizing fluids or fluidsthat coke.
H h r r n .
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Crystallizing fluids orfluids that salt out.
Caustic.
Cold fluids less than 32
F (0 C).
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Plan 62Plan 62Preventative Maintenance Quench inlet should be on
top of gland with drain/outlet
on bottom. Quench pressure should be
limited to 3 psi (0.2 bar) orless.
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Use throttle bushing on
atmospheric side of seal todirect quench flow to sealdrain.
Monitor regularly, checkingfor closed valves, blocked
lines, and steam trapcondition.
PlPl
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Plan 72Plan 72What
Unpressurizedbuffer gas controlsystem.
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Containment sealsupport typicallywith nitrogen buffergas.
Pl 72Pl 72
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Plan 72Plan 72Why
Zero to very lowprocess emissions.
f k
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primary seal.
Pl 72Pl 72
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Plan 72Plan 72Where
Used with dualunpressurized containmentseals (tandem).
High vapor pressure fluids,light hydrocarbons.
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Hazardous or toxic fluids.
Clean, non-polymerizing,non-oxidizing fluids.
Used in combination withPlan 75 and/or Plan 76.
Pl 72Pl 72
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Plan 72Plan 72Preventative Maintenance Clean, reliable, low pressure
gas must be supplied to seal
at all times. Bottled gas supply is not
recommended except asart of an emer enc
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backup system.
Primary seal leakage isindicated by pressure in thevent line.
Vent or drain are usuallyconnected to low pressurevapor recovery/flare system.
Pl 74Pl 74
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Plan 74Plan 74What
Pressurized barriergas control system.
l r
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typically withnitrogen barrier gas.
Pl 74Pl 74
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Plan 74Plan 74Why
Isolate process fluid.
Zero processmi i n .
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Pl 74Pl 74
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Plan 74Plan 74Where
Used with dual pressurizedgas seals (double).
High vapor pressure fluids,light hydrocarbons.
Hazardous or toxic fluids.
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Services that do not tolerate
barrier fluids. Clean, non-polymerizing
fluids.
Moderate temperature fluids.
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Plan 75Plan 75
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Plan 75Plan 75What
Drain from containment
seal cavity to liquidcollector and vapor
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.
Plan 75Plan 75
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Plan 75Plan 75Why
Leakage collectionfor zero to very lowprocess emissions.
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Safety indicator forprimary seal.
Plan 75Plan 75
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Plan 75Plan 75Where
May be used alone or withPlan 72 on containment
seals. Fluids that condense at
ambient temperature.
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High pressure fluids, light
hydrocarbons. Hazardous or toxic fluids.
Clean, non-polymerizing,non-oxidizing fluids.
Plan 75Plan 75
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Plan 75Plan 75Preventative Maintenance
Collection reservoir must belocated below seal drain and
downward-sloped piping. Continuously vent collection
reservoir to low pressure
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vapor recovery/flare system.
Drain collection reservoir toliquid recovery system asneeded.
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Plan 76Plan 76
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Plan 76Plan 76What
Vent fromcontainment sealcavity to vapor
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recovery.
Plan 76Plan 76
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Plan 76Plan 76 Why
Leakage collectionfor zero to very lowprocess emissions.
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Safety indicator forprimary seal.
Plan 76Plan 76
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Plan 76Plan 76Where
May be used alone or withPlan 72 on containment
seals. Fluids that do not condense
at ambient temperature.
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High vapor pressure fluids,
light hydrocarbons. Hazardous or toxic fluids.
Clean, non-polymerizing,non-oxidizing fluids.
Plan 76Plan 76
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Plan 76Plan 76Preventative Maintenance
Continuously vent to lowpressure vapor
recovery/flare system. Vent piping should include a
condensate drain.
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Primary seal leakage is
detected by increased ventpressure.
Monitor regularly for valvesettings, blocked lines, andlow vent pressure.
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Good Piping PracticesGood Piping PracticesMinimize line losses Plan 53A Example
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Large diameter tubing
Upward sloping lines
Long radius bends
Vertical
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qu pmen
HorizontalEquipment
- n.(0.45 - 0.6 m)
4 ft. (1.2 m) max
low point drain
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ReviewReview Intended to create a more favorable environment for
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Intended to create a more favorable environment forthe seal
Collect and detect seal leakage and provide safetybackup
Documented in several API, ASME, and ISO
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standards
May require auxiliary equipment or external sourcesof fluids
Necessary to improve seal reliability
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Flow Solutions Success Cycle
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