GPSA Engineering Data Book 14th Edition

REVISION DATE REASON(S) FOR REVISION0 4/1/2017 Initial release

GPSA Engineering Data Book 14th Edition

FIG. 7-1Nomenclature

A = MW =

= NILL =

= NLL =

C' = drag coefficient of particle, dimensionless (Fig. 7-3) Nref =D = Vessel diamter, ft =

= Characteristic diameter in Stoke Number, St OD == Liquid hydraulic diameter, ft P == droplet diameter, ft =

= Nozzel diamter, ft == Droplet size (micron) for 95% removal =

g = R =

GOR = Gas-oil ratio Re =

H = Height, ft Stk =

= Settling height, ft T =HILL = High interphase liquid level t =

HHILL = High- high interphase liquid level V =HLL = High liquid level =

HHLL = High- high liquid level =

J = =

K = empirical constant for separator sizing, ft/sec == =

L = seam to seam length of vessel, ft =

= =

LILL = Low interphase liquid level =LLILL = Low-low interphase liquid level Z =LLL = Low liquid level Greek

LLLL = Low-low liquid levelβ =

= mass of droplet or particle, lb ==

=

area, ft2

Amesh Mesh pad area, ft2

Ap particle or droplet cross sectional area, ft2

Nμ

Dc

Dh

Dp QA

d2 Q1

d95 Q1,max

acceleration due to gravity, 32.2 ft/sec2

Hset

Vc

Vh

gas momentum, lb/(ft•sec2) V1

Vr

KCR proportionality constant from Fig. 7-4 for use in Eq 7-5, dimensionless

Vr,max

Vt

Lset Effective gravity droplet settling length for a horizontal separator, ft

Wg

W1

Mp ρc

ρg

ρl

=

=

===

==

==

σ =φ =

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

ρhl

ρll

ρm

ρp

μc

μg

μhl

μll

μ1

FIG. 7-1Nomenclature

molecular weight, lb/lb mole

Normal interphase liquid level

Normal liquid level

Reynolds film numberInterfacial viscosity numberOutside diamter, insystem pressure, psia

Reynolds number, dimensionless

retention time, minutesVelocity, ft/secVelocity of continuous phase, ft/sec

Liquid velocity, ft/sec

Gas velocity relative to liquid, ft/sec

Flow rate of gas, lb/hr

Flow rate of liquid, lb/hrcompressibility factor, dimensionless

Greek

actual gas flow rate, ft3/sec

Liquid volumetric flow rate, ft3/minMaximum liquid volumetric flow rate, ft3/min

gas constant, 10.73 (psia•ft3)(°R•lb mole)

Dimensionless Stokes Number: [g • pc • Vc • D2p]/(18μc • Dc)

system temperature, °R

Flow vapor velocity between gas-liquid interphase and the top of a horizontal separator, ft/sec

Maximum velocity of a gas relative to liquid to resist substantial re-entreainment

critical or terminal gas velocity necessary for particles of size Dp to drop or settle out of gas, ft/sec

Ratio of the number of influent particles of a given size to the number of effluent particles of the same size

Continuous phase density, lb/ft3

gas phase density, lb/ft3

liquid phase density, droplet or particle, lb/ft3

viscosity of continuous pase, Cp

Gas viscosity, cPHeavy liquid phase viscosity, cP

Light liquid phase viscosity, cPLiquid viscosity, cPLiquid surface tension, dynes/cmFlow parameter

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

Heavy liquid phase density, lb/ft3

Light liquid phase density, lb/ft3

Mixed fluid density, lb/ft3

Droplet or partical phase density, lb/ft3

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.

In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.

These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.

GPSA Engineering Data Book 14th Edition

Given: = 2.07 = 0.012 cP= 31.2= 150 microns

Calculations:= 150*0.00003937/12=0.000492 ft

== 1.35

= ft/sec

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

Example 7-1 -- Calculate the terminal velocity using the drag coefficient and Stokes' Law terminal settling velocity in a vertical gas-liquid separator for a 150 micron particle for a fluid with the physical properties listed below.

ρg lb/ft3

μg

ρl lb/ft3

Dp

Dp

C' (Re)2 0.95*108*2.07*(0.0004923•(31.2 - 2.07)/0.0122=4741C'

Vt (4*32.2*0.000492*(31.2-2.07)/(3*2.07*1.35))0.5=0.47

Given: = 2.07 = 0.012= 31.2= 150

Calculations:= 0.000492

(from Eq. 7-4) = 4,741(from Fig.7-5) = 1.35

(from Eq. 7-1) = 0.47

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

Example 7-1 -- Calculate the terminal velocity using the drag coefficient and Stokes' Law terminal settling velocity in a vertical gas-liquid separator for a 150 micron particle for a fluid with the physical properties listed below.

Application 7-1 -- Calculate the terminal velocity using the drag coefficient and Stokes' Law terminal settling velocity in a vertical gas-liquid separator for a 150 micron particle for a fluid with the physical properties listed below.

ρg

μg

ρl

Dp

Dp

C' (Re)2

C'Vt

cP

microns

ft

(from Eq. 7-4)(from Fig.7-5)

ft/sec (from Eq. 7-1)

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

Application 7-1 -- Calculate the terminal velocity using the drag coefficient and Stokes' Law terminal settling velocity in a vertical gas-liquid separator for a 150 micron particle for a fluid with the physical properties listed below.

lb/ft3

lb/ft3

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.

In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.

These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.

GPSA Engineering Data Book 14th Edition

Operating Conditions and DesignGas molecular weight = 17.55

Operating temperature = 120Operating pressure = 500

Gas flowrate = 150Liquid flowrate = 100

Design Factor = 10%Souder-Brown K-value = 0.35

Inlet device = DiffuserInternals = Mist eliminator

Vapor outlet configuration = Nozzle above top headAllowance for support ring = 4.00

Inlet piping OD = 18.00Inlet piping ID = 16.876

Bottom tangent to LLLL = 18.0LLLL to LL surge time = 1.0LLL to HLL surge time = 5.0

HLL to HHLL surge time = 1.0

Physical Properties = 1.552 = 0.013= 44.68= 0.574

= 1.75Vessel Diameter Sizing

= 17.55*150*1000000/24/379.47=289054= 100*60/7.4805*44.68=35837= 289054/1.552/3600*(1+0.1)=56.91

Corrected K-value = 0.82*0.35=0.29= 0.29*SQRT((44.68-1.552)/1.552)=1.51

D =

A = 3.14159*(7.5/2)^2=44.2Liquid Surge Section

Q = 35837/44.68/60*(1+0.1)=14.7LLL to HLL = 14.7/44.2*5*12=20.0

LLLL to LLL = 14.7/44.2*1*12=4.0

Example 7-2 -- Determine the size of a vertical gas-liquid separator with a high efficiency wire mesh mist eliminator to handle 150 MMSCFD (MW= 17.55) of gas and 100 gpm of condensate. A design factor of 10% will be used.

ρg

μg

ρl

μl

ρm

Wg

Wl

QA

Vmax

(4*56.91/3.1416/1.51)0.5+4/12=7.26

HLL to HHLL = 14.7/44.2*1*12=4.0LLLL to HHLL = (20+4+4)/12=2.3

Check De-Gassing (200 micron bubble)= 14.7/44.2/60=0.006= 1.145/1000*(44.68-1.552)/0.574=0.086

De-Gassing: can occurCheck Inlet Velocity Head for Nozzle size

V = (289054+35837)*144/1.75/3.1416/(16.876/2)^2/3600=33.2J = 1.75*33.2^2=1929

Vessel Lengths= 18/12+2.5=4.0= 2.00= 1.50= 3.00= 0.50= 7.26/4=1.82 use 2.0

Demister to Oulet Nozzle = 7.5/2-16.876/2/12=3.05Total Vessel Length = 4+2+1.5+3+0.5+2=13.0

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

V1

Vt

H1 + H2

H3

H4

H5

H6

H7

lbm/lbmole°FpsigMMSCFDgpm

ft/sec (Figure 7-35a)

(Figure 7-38)inchinchinchinchminminmin

cP

cP

lb/hrlb/hr

ft/sec (K is corrected for pressure using Fig. 7-36)ft/sec (Equation 7-11)

(Equation 7-18, rounded up to 7.5 ft)

inchinch

Example 7-2 -- Determine the size of a vertical gas-liquid separator with a high efficiency wire mesh mist eliminator to handle 150 MMSCFD (MW= 17.55) of

lb/ft3

lb/ft3

lb/ft3

ft3/sec

ft

ft2

ft3/min

inchft (rounded up to 2.5 ft)

ft/sec Equation 7-16aft/sec Equation 7-17

ft/sec

acceptable

ft (bottom tangent to HHLL)ft (HHLL to Feed nozzle bottom)ft (Feed nozzle diameter)ft (Feed nozzle top to mist eliminator bottom)ft (Feed nozzle top to mist eliminator bottom)ft (per Fig. 6-23 for elliptical 2:1 heads)ft (Figure 7-38)ft (total length tangent-to-tangent)

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

lb/ft•sec2

Operating Conditions and DesignGas molecular weight = 17.55 lbm/lbmole

Operating temperature = 120 °FOperating pressure = 500 psig

Gas flowrate = 150 MMSCFDLiquid flowrate = 100 gpm

Design Factor = 10%Souder-Brown K-value = 0.35 ft/sec

Inlet device = DiffuserInternals = Mist eliminator

Vapor outlet configuration = Nozzle above top headAllowance for support ring = 4.00 inch

Inlet piping OD = 18.00 inchInlet piping ID = 16.876 inch

Bottom tangent to LLLL = 18.0 inchLLLL to LL surge time = 1.0 minLLL to HLL surge time = 5.0 min

HLL to HHLL surge time = 1.0 min

Physical Properties = 1.552 = 0.013 cP= 44.68= 0.574 cP= 1.75

Vessel Diameter Sizing= 289,054 lb/hr= 35,837 lb/hr= 56.91

Corrected K-value = 0.29 ft/sec = 1.51 ft/sec

D = 7.50

A = 44.2Liquid Surge Section

Q = 14.70LLL to HLL = 20.0 inch

LLLL to LLL = 4.0 inch

Application 7-2 -- Determine the size of a vertical gas-liquid separator with a high efficiency wire mesh mist eliminator to handle 150 MMSCFD (MW= 17.55) of gas and 100 gpm of condensate. A design factor of 10% will be used.

ρg lb/ft3

μg

ρl lb/ft3

μl

ρm lb/ft3

Wg

Wl

QA ft3/sec

Vmax

ft

ft2

ft3/min

HLL to HHLL = 4.0 inchLLLL to HHLL = 2.5 ft

Check De-Gassing (200 micron bubble)= 0.006 ft/sec= 0.086 ft/sec

De-Gassing: can occurCheck Inlet Velocity Head for Nozzle size

V = 33.2 ft/secJ = 1,929

Vessel Lengths= 4.00 ft= 2.00 ft= 1.50 ft= 3.00 ft= 0.50 ft= 2.00 ft

Demister to Oulet Nozzle = 3.05 ftTotal Vessel Length = 13.00 ft

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

V1

Vt

lb/ft•sec2

H1 + H2

H3

H4

H5

H6

H7

(Figure 7-35a)

(Figure 7-38)

(K is corrected for pressure using Fig. 7-36)(Equation 7-11)

(Equation 7-18, rounded up to 0.5 ft)

Application 7-2 -- Determine the size of a vertical gas-liquid separator with a high efficiency wire mesh mist eliminator to handle 150 MMSCFD (MW= 17.55) of

Equation 7-16aEquation 7-17

acceptable

(bottom tangent to HHLL)(HHLL to Feed nozzle bottom)(Feed nozzle diameter)(Feed nozzle top to mist eliminator bottom)(Feed nozzle top to mist eliminator bottom)(per Fig. 6-23 for elliptical 2:1 heads)(Figure 7-38)(total length tangent-to-tangent)

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.

In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.

K values FPS K values SI Inlet device Outlet config. Internals0.35 0.11 Diffuser Nozzle above top head Mist eliminator0.40 0.12 Baffle Side nozzle above demister0.45 0.14 Elbow Side nozzle below demister0.50 0.15 Half-pipe 0.55 0.17 Cyclone 0.60 0.18 None 0.65 0.20 0.70 0.21 0.75 0.23 0.80 0.24 0.85 0.26 0.90 0.27 0.95 0.29 1.00 0.30

GPSA Engineering Data Book 14th Edition

Operating temperature = Operating pressure =

Gas flowrate =Liquid flowrate =

= = ===

Gas MW =

LLLL to LLL =LLLL to NLL =

LLL to HLL =HLL to HHLL =

Type =Design driven by =Inlet nozzle type =

LLLL height =Length/Diameter ratio =

Assumed partial volume to LLLL =Assumed partial volume to HHLL =

Inlet nozzle ID =Outlet gas nozzle ID =

Flow rates --Gas flowrate =

Liquid flowrate =

Surge time =Total volume of vessel =

Vessel internal diameter =Vessel length (tangent-to tangent) =

H/D at LLLL =Calculated partial volume to LLLL =

Application 7-3 -- Determine the configuration and size of a separator vessel to provide surge upstream of a process unit and to separate liquids and gas. The stream is 25,000 bpd of condensate and 15 MMSCFD of gas (MW = 17.55). Process conditions are as follows:

Operating Conditions --

Physical Properties --ρg

μg

ρl

μ1

ρm

Project Surge Times --

Assumptions for vessel sizing --

Vessel sizing -- Including the liquid volume stored in the vessel's heads

Liquid Level Calculation --

Partial volume to LLLL height =Surge volume (LLLL to HHLL) =Partial volume to HHLL height =

Volume fraction to HHLL height =H/D at HHLL =HHLL height =

Volume fraction at NLL =H/D at NLL =NLL height =

Gas flow area =Average gas velocity =

Flow factor =

De-gassing =Calculate Mesh Pad Area & Height --

K factor for high efficiency eliminator =De-rated K factor =

==

Check Nozzles Head --Inlet nozzle velocity =

Inlet nozzle momentum =

Inlet nozzle size =

Outlet gas nozzle velocity =

Outlet gas nozzle momentum =

Outlet gas nozzle size =

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

Check Gas flow factor @ HHLL in Gravity Separation Section --

Check De-Gassing --

Vmax

Amesh

120250 psig15 MMSCFD

25,000 bpd

0.774

0.01244.58 lb/ft30.573 cP

6.87 lb/ft317.55 lb/lbmol

1.0 min3.5 min5.0 min1.0 min

horizontalhigh liquid flowrate

diffuser18.00 inches3.0010%70%

10.020 inches6.065 inches

15*1000000/24/379.47*17.55=28905 lb/hr25000*5.615/24*44.58=260747 lb/hr

1+5+1=7 min260747/60/44.58*7/(0.70-0.10)=1137

ft8*3.0=24 ft

18/12/8=0.187513%

Application 7-3 -- Determine the configuration and size of a separator vessel to provide surge upstream of a process unit and to separate liquids and gas. The stream is 25,000 bpd of condensate and 15 MMSCFD of gas (MW = 17.55). Process conditions are as follows:

°F,

lb/ft3

lb/ft3

Including the liquid volume stored in the vessel's heads

ft3

4*1137/3.1416/3/(1+1/(3*3))0.333=7.6

0.13*1137=143(0.70-0.10)*1137=682

143+682=826826/1137*100=73%

0.6790.679*8=5.43 ft

25000*5.615/1440*3.5/1137+0.13=0.4260.443

0.443*8=3.54 ft

28905/0.774/13.8/3600=0.75 ft/secft/sec

Not an issue

0.35 ft/sec0.89*0.35=0.31 ft/sec

0.31*SQRT(44.58/0.774-1)=2.35 ft/sec28905/0.774/3600/2.35=4.41

ft/sec

Acceptable

ft/sec

Acceptable

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

ft3

ft3

ft3

Check Gas flow factor @ HHLL in Gravity Separation Section --(1-0.73)*3.14159*(8/2)2=13.8 ft2

0.75*((44.58-0.774)/0.774)-0.5=0.100

ft2

(28905+260747)*144*1/(6.87*1*3.14159*(10.02/2)2*3600)=21.4

6.87*21.42=3142 lb/ft•sec2

28905*144*1/0.774/1/3.14159/(6.065/2)2/3600=51.7

0.774*51.72=2069 lb/ft•sec2

Operating temperatureOperating pressure

Gas flowrateLiquid flowrate

Gas MW

LLLL to LLLLLLL to NLL

LLL to HLL(7 min surging from LLLL to HHLL) HLL to HHLL

TypeDesign driven byInlet nozzle type

LLLL heightLength/Diameter ratio

Assumed partial volume to LLLLAssumed partial volume to HHLL

Inlet nozzle IDOutlet gas nozzle ID

Flow rates --Gas flowrate

0.126046981600838 Liquid flowrate

Surge timeTotal vessel capacity

(rounded up to 8 ft) Vessel internal diameterVessel length (tangent-to tangent)

H/D at LLLL(using Figs. 6-24 & 6-25 w/H/D=0.1875) Calculated partial volume to LLLL

Application 7-3 -- Determine the configuration and size of a separator vessel to provide surge upstream of a process unit and to separate liquids and gas. The stream is 25,000 bpd of Application 7-3 -- Determine the configuration and size of a separator vessel to provide surge upstream of a process unit and to separate liquids and gas. The stream is 25,000 bpd of condensate and 15 MMSCFD of gas (MW = 17.55). Process conditions are as follows:

Operating Conditions --

Physical Properties --ρg

μg

ρl

μ1

ρm

Project Surge Times --

Assumptions for vessel sizing --

Vessel sizing -- Including the liquid volume stored in the vessel's heads

Liquid Level Calculation --

Partial volume to LLLL heightSurge volume (LLLL to HHLL)Partial volume to HHLL height

Volume fraction to HHLL height(using Figs. 6-24 & 6-25) H/D at HHLL

HHLL heightVolume fraction at NLL

(using Figs. 6-24 & 6-25 w/H/D=0.426) H/D at NLLNLL height

Gas flow areaAverage gas velocity

(Acceptable gas area, flow factor<0.5 ft/s) Flow factor

(7 min > 2 min) De-gassingCalculate Mesh Pad Area & Height --

K factor for high efficiency eliminator(with help from Fig.7-36) De-rated K factor(Equation 7-11)(Equation 7-13)

Check Nozzles Head --Inlet nozzle velocity

Inlet nozzle momentum

Inlet nozzle size

Outlet gas nozzle velocity

Outlet gas nozzle momentum

Outlet gas nozzle size

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

Check Gas flow factor @ HHLL in Gravity Separation Section --

Check De-Gassing --

Vmax

Amesh

(momentum<6000 lb/ft•sec2)

(momentum<6000 lb/ft•sec2)

= 120 = 250 psig= 15 MMSCFD= 25,000 bpd

= 0.774 = 0.012= 44.58 lb/ft3= 0.573 cP= 6.87 lb/ft3= 17.55 lb/lbmol

= 1.0 min= 3.5 min= 5.0 min= 1.0 min

= horizontal= high liquid flowrate= diffuser= 18.00 inches= 3.00= 10%= 70%= 10.020 inches= 6.065 inches

= 28,905 lb/hr= 260,747 lb/hr

= 7.0 min= 1,137= 8.0 ft = 24.0 ft

= 0.1875= 13%

Application 7-3 -- Determine the configuration and size of a separator vessel to provide surge upstream of a process unit and to separate liquids and gas. The stream is 25,000 bpd of condensate and 15 MMSCFD of gas (MW = 17.55). Process conditions are as follows:

°F,

lb/ft3

lb/ft3

Including the liquid volume stored in the vessel's heads

ft3

= 143= 682= 826= 73%= 0.679= 5.43 ft= 0.426= 0.443= 3.54 ft

= 13.8= 0.75 ft/sec= 0.100 ft/sec

= Not an issue

= 0.35 ft/sec= 0.31 ft/sec= 2.35 ft/sec= 4.41

= 21.4 ft/sec

= 3,142

= Acceptable

= 51.7 ft/sec

= 2,069

= Acceptable

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

ft3

ft3

ft3

Check Gas flow factor @ HHLL in Gravity Separation Section --ft2

ft2

lb/ft•sec2

lb/ft•sec2

(rounded up)

(using Figs. 6-24 & 6-25 w/H/D=0.1875)

Application 7-3 -- Determine the configuration and size of a separator vessel to provide surge upstream of a process unit and to separate liquids and gas. The stream is 25,000 bpd of condensate and 15 MMSCFD of gas (MW = 17.55). Process conditions are as follows:

(using Figs. 6-24 & 6-25)

(using Figs. 6-24 & 6-25)

(using Figs. 6-24 & 6-25\)

(Aceptable gas area)

(Equation 7-11)(Equation 7-13)

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.

In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

(momentum<6000 lb/ft•sec2)

(momentum<6000 lb/ft•sec2)

While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.

In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.

GPSA Engineering Data Book 14th Edition

Example 7-4 -- Provide a vessel to separate gas, light liquid, and heavy liquid at the conditions given below.

Operating pressure = Gas flowrate =

Light liquid flowrate =Heavy liquid flowrate =

Liquid droplet removal size (liq/liq separation) =Heavy liquid retention time (Bottom-NILL) =

Light liquid retention time (NILL-NLL) =Liquid surge time (LLL to HLL) =Liquid surge time (LLL to HLL) =

HHLL (% of full volume) =Light surge time fraction (NLL to HLL) =

Time between HLL and HHLL =Settling chamber L/D =

Standpipe =Type =

Separator sizing driver =LLILL elevation above boot bottom =

LILL elevation above LLILL =NILL elevation above LILL =HILL elevation above NILL =

Standpipe elevation above HILL =LLL elevation above Standpipe =

HHLL elevation above HLL =

= = =

= ==

Flow rates --Light liquid flowrate =

Heavy liquid flowrate =Vessel sizing --

Total volume =

Internal diameter =

Calculate Levels (ignoring heads volume) --LLILL elevation above boot bottom =

Design Basis --

Physical Properties --

ρg

μg

ρll

μll

ρhl

μhl

LILL elevation above boot bottom =Preliminary volume fraction to NILL elevation =Preliminary NILL elevation above boot bottom =

NILL elevation above boot bottom =Volume fraction to NILL elevation =HILL elevation above boot bottom =Volume fraction to HILL elevation =

Standpipe elevation above boot bottom =LLL elevation above boot bottom =Volume fraction to LLL elevation =Volume fraction to NLL elevation =NLL elevation above boot bottom =Volume fraction to HLL elevation =HLL elevation above boot bottom =

HHLL elevation above boot bottom =Stokes's Law Analysis for Heavy Oil Particles Settling Through Light Oil Phase (NLL to NILL levels) --

Maximum settling velocity =Settling time required =

Available settling time =Settlement of larger heavy oil particles

Max. axial-velocity =Stokes's Law Analysis for Light Oil Particles Rising Through Heavy Oil Phase (Bottom to NILL) --

Maximum settling velocity =Settling time required =

Available settling time =Settlement of larger light oil particles

Max. axial-velocity =

Heavy phase retention time (bottom to HILL) =Stokes' Law settling time =

Settling process in heavy-phase =

Light phase retention time (NILL to LLL) =Stokes' Law settling time =

Settling process in light-phase =

Light phase retention time (HILL to NLL) =Stokes' Law settling time =

Settling process in light-phase =

Light phase retention time (NILL to HLL) =Stokes' Law settling time =

Settling process in light-phase =

Inlet zone to include 2 distribution baffles =

Check Settling Time for Off- Normal Level Operation --

Calculate Final Vessel Length --

Heads, one at each end =Outlet zone (outlet liquid nozzle) =

Tangent-to tangent length =Total length =

Terminal velocity =

Calculated Souders-Brown K-value =Typical derated K-value for wire mesh mist eliminator =

Gas section separtion

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

Gravity Separation and Gas Polishing Section --

Example 7-4 -- Provide a vessel to separate gas, light liquid, and heavy liquid at the conditions given below.

250 psig10.0 MMSCFD

26,900 bpd5,181 bpd150 micron10 min10 min5 min, or12 inch

70%50%

1 min3.00Yes

horizontalLiquid surge

12.0 inch (min. 12 inches)4.0 inch (min. 4 inches)6.0 inch (min. 6 inches)6.0 inch6.0 inch12.0 inch4.0 inch

0.7740.020 cP43.7 lb/ft30.31 cP61.9 lb/ft30.65 cP

26900*5.615/24=6293

5181*5.615/24=1212

(6293*(10+5*0.5+1)/60+1212*10/60)/0.7=2312(2312/3.1416/(1/12+3/4))^(1/3)=10 ft

12/12=1.0 ft (min. 12 inches)

lb/ft3

ft3/hr

ft3/hr

ft3

1+4/12=1.33 ft (4 inches above LLILL)1212*10/60/2312=0.087 (H/D≈0.14 from Fig.6-24)

0.14*10=1.4 ft1.33+6/12=1.83 ft (min. 6 inches above LILL)

0.125 (H/D≈0.183 from Fig.6-24)1.4+6/12=1.9 ft

0.135 (H/D≈0.19 from Fig.6-24)1.9+6/12=2.4 ft2.4+12/12=3.4 ft

0.299 (from Fig.6-24 w/H/D≈0.34)6293*10/60/2312+0.125=0.579 (H/D≈0.562 from Fig.6-24)

0.579*10=5.8 ft6293*2.5/60/2312+0.579=0.692 (H/D≈0.65 from Fig.6-24)

0.65*10=6.50 ft6.5+4/12=6.83 ft (4 inches above HLL)

Stokes's Law Analysis for Heavy Oil Particles Settling Through Light Oil Phase (NLL to NILL levels) --10.0 inch/min

(5.8-1.83)/C55*12=4.8 min10.0 min

Acceptable (10 min > 4.8 min)ft/min

Stokes's Law Analysis for Light Oil Particles Rising Through Heavy Oil Phase (Bottom to NILL) --10.0 inch/min

(1.83-0)/C55*12=2.2 min10.0 min

Acceptable

ft/min

0.135*2312*60/1212=15.5 min1.9/(10/12)=2.3 min

Aceptable

(0.35-0.125)*2312/6293*60=5.0 min(3.4-1.83)/(10/12)=1.9 min

Acceptable

(0.579-0.135)*2312/6293*60=9.8 min(5.8-1.9)/(10/12)=4.7 min

Acceptable

(0.692-0.125)*2312/6293*60=12.5 min(6.5-1.83 )/10*12=5.6 min

Acceptable

0.5*10=5.0 ft

1212/60/0.125/(3.1416*(10/2)2)=2.1

6293/60/(0.579-0.125)/(3.1416*(10/2)2)=2.9

2*10/4=5.0 ft 0.25*10=2.5 ft 10*3=30.0 ft

5+5+2.5+30=37.5 ft

1488*32.2*(150*0.00003937/12)^2*(43.7-0.774)/18/0.02=1.4 ft/s

ft/s0.360 ft/s

Acceptable

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

1.4/((43.7-0.774)/0.774)0.5=0.188

Operating pressure = 250Gas flowrate = 10.0

Light liquid flowrate = 26,900Heavy liquid flowrate = 5,181

Liquid droplet removal size (liq/liq separation) = 150Heavy liquid retention time (Bottom-NILL) = 10

Light liquid retention time (NILL-NLL) = 10Liquid surge time (LLL to HLL) = 5Liquid surge time (LLL to HLL) = 12

HHLL (% of full volume) = 70%Light surge time fraction (NLL to HLL) = 50%

Time between HLL and HHLL = 1Settling chamber L/D = 3.00

Standpipe = YesType = horizontal

Separator sizing driver = Liquid surgeLLILL elevation above boot bottom = 12.0

LILL elevation above LLILL = 4.0NILL elevation above LILL = 6.0HILL elevation above NILL = 6.0

Standpipe elevation above HILL = 6.0LLL elevation above Standpipe = 12.0

HHLL elevation above HLL = 4.0

= 0.774 = 0.020= 43.7

= 0.31= 61.9= 0.65

Flow rates --Light liquid flowrate = 6,293

Heavy liquid flowrate = 1,212Vessel sizing --

Total volume = 2,312Internal diameter = 10.00

LLILL elevation above boot bottom = 1.00

Application 7-4 -- Provide a vessel to separate gas, light liquid, and heavy liquid at the conditions given below.Design Basis --

Physical Properties --

ρg

μg

ρll

μll

ρhl

μhl

Calculate Levels (including heads volume) --

LILL elevation above boot bottom = 1.33Preliminary volume fraction to NILL elevation = 0.087Preliminary NILL elevation above boot bottom = 1.46

NILL elevation above boot bottom = 1.83Volume fraction to NILL elevation = 0.122HILL elevation above boot bottom = 2.0Volume fraction to HILL elevation = 0.135

Standpipe elevation above boot bottom = 2.5LLL elevation above boot bottom = 3.5Volume fraction to LLL elevation = 0.304Volume fraction to NLL elevation = 0.576NLL elevation above boot bottom = 5.6Volume fraction to HLL elevation = 0.576HLL elevation above boot bottom = 5.8

HHLL elevation above boot bottom = 6.1Stokes's Law Analysis for Heavy Oil Particles Settling Through Light Oil Phase (NLL to NILL levels) --

Maximum settling velocity = 10.0Settling time required = 4.9

Available settling time = 10.0Settlement of larger heavy oil particles Acceptable

Max. axial-velocity = 2.1Stokes's Law Analysis for Light Oil Particles Rising Through Heavy Oil Phase (Bottom to NILL) --

Maximum settling velocity = 10.0Settling time required = 2.2

Available settling time = 10.0Settlement of larger light oil particles Acceptable

Max. axial-velocity = 3.0

Heavy phase retention time (bottom to HILL) = 15.4Stokes' Law settling time = 2.4

Settling process in heavy-phase = Acceptable

Light phase retention time (NILL to LLL) = 4.8Stokes' Law settling time = 2.0

Settling process in light-phase = Acceptable

Light phase retention time (HILL to NLL) = 9.7Stokes' Law settling time = 4.3

Settling process in light-phase = Acceptable

Light phase retention time (NILL to HLL) = 10.0Stokes' Law settling time = 4.7

Settling process in light-phase = Acceptable

Inlet zone to include 2 distribution baffles = 5.0

Check Settling Time for Off- Normal Level Operation --

Calculate Final Vessel Length --

Heads, one at each end = 5.0Outlet zone (outlet liquid nozzle) = 2.5

Tangent-to tangent length = 30.0Total length = 42.5

Terminal velocity = 1.4

Calculated Souders-Brown K-value = 0.186Typical derated K-value for wire mesh mist eliminator = 0.360

Gas section separtion Acceptable

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.The Calculation Spreadsheets are provided without warranty of any kind including warranties of accuracy or reasonableness of factual or scientific assumptions, studies or conclusions, or merchantability, fitness for a particular purpose, or non-infringement of intellectual property.In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

Gravity Separation and Gas Polishing Section --

psigMMSCFDbpdbpdmicronminminmin, orinch

min

inch (min. 12 inches)inch (min. 4 inches)inch (min. 6 inches)inchinchinchinch

cPlb/ft3 cPlb/ft3 cP

ft

ft (min. 12 inches)

Application 7-4 -- Provide a vessel to separate gas, light liquid, and heavy liquid at the conditions

lb/ft3

ft3/hr

ft3/hr

ft3

ft (4 inches above LLILL)

ftft

ft

ftft

ft

ftft

Stokes's Law Analysis for Heavy Oil Particles Settling Through Light Oil Phase (NLL to NILL levels) --inch/minminmin

ft/minStokes's Law Analysis for Light Oil Particles Rising Through Heavy Oil Phase (Bottom to NILL) --

inch/minminmin

ft/min

minmin

minmin

minmin

minmin

ft

ft ft ft ft

ft/s

ft/sft/s

The sample calculations, equations and spreadsheets presented herein were developed using examples published in the Engineering Data Book as published by the Gas Processors Suppliers Association as a service to the gas processing industry. All information and calculation formulae has been compiled and edited in cooperation with Gas Processors Association (GPA).While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.

In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.

In no event will the GPA or GPSA and their members be liable for any damages whatsoever (including without limitation, those resulting from lost profits, lost data or business interruption) arising from the use, inability to, reference to or reliance on the information in this Publication, whether based on warranty, contract, tort or any other legal theory and whether or not advised of the possibility of such damages.These calculation spreadsheets are provided to provide an “Operational level” of accuracy calculation based on rather broad assumptions (including but not limited to: temperatures, pressures, compositions, imperial curves, site conditions etc) and do not replace detailed and accurate Design Engineering taking into account actual process conditions, fluid properties, equipment condition or fowling and actual control set-point dead-band limitations.

While every effort has been made to present accurate and reliable technical information and calculation spreadsheets based on the GPSA Engineering Data Book sample calculations, the use of such information is voluntary and the GPA and GPSA do not guarantee the accuracy, completeness, efficacy, or timeliness of such information. Reference herein to any specific commercial product, calculation method, process, or service by trade-name, trademark, and service mark manufacturer or otherwise does not constitute or imply endorsement, recommendation or favoring by the GPA and/or GPSA.