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SECTION 1

General Information

This section includes a br ief descript ion of th e techn ical ac-tivities of the Gas Processors Association (GPA) and the GasPr ocessors Sup pliers Associat ion (GPSA). It includes a com-pilation of curr ent GPA stan dar ds, publications a nd Resear chReport s, a glossar y of terms used in t he gas pr ocessing indus-try and several tables of common conversion factors andequivalents. At the end of the Section is a listing of other t ech-nical associations an d societies tha t pu blish codes, stan dard san d other informat ion pertinen t to the natu ral gas processingindustry.

GPA TECHNICAL ACTIVITIES

The Gas Processors Association is an intern ational organi-zation with a membership of about 135 companies, each ofwhich is engaged in one or more functions of the na tur al gasand gas processing industry, including: natural gas produc-tion, gath ering a nd pr ocessing; production of natu ra l gas liq-uids (NGLs); volume transport or further processing ofnatural gas or gas liquids; or other commerce in natural gasor gas liquids. Its principal functions include t he a dvancementof gas processing t echnology thr ough development and prom-ulgation of intern at ional st an dar ds for NGL product specifi-cations, test methods, measurement, and handling. Inaddition, GPA sponsors basic research in t herm odynam ic an dtransport properties of natural gases, gas liquids, syntheticgases, and related process stream components. The dissemi-na tion of GPA techn ology is accomplish ed t hr ough pu blicat ionof industry standards, research reports, and computer pro-gram s. This t echnology is developed in r esponse to indust ry

needs by a technical committee organizat ion with th e follow-ing structu re an d responsibilities:

Techn ical Committee The par ent body responsiblefor assessin g th e technological needs of the gas pr ocessingindust ry, establishing pr iorities, ass igning pr oblems t o appro-priat e working sections, and r eviewing results an d recommen -dat ions of sections a s n eeded.

The seven working sections of th e Technical Comm ittee a re:

Section A, Facil it ies Design and Optimization Mainta ins a continu ing study of all phases of gas processingdesign (process, mechanical, electrical, instrumentation) ofbroad industry interest; this responsibility does not includean alytical meth ods nor basic dat a on product properties, but

does include onstream process and plan t contr ol instr ument a-tion.

Section B, Analysis Studies and develops analyticalprocedures and meth ods to improve accura cy an d reliabilityof test m ethods and da ta to meet the n eeds of the gas process-ing indus tr y. All of the indu str ys sam pling procedures , speci-fication test methods, and analytical standards have issuedfrom th is section.

Section C, Specifications Maintains existing pr oductspecifications, and generates new and revised specifications

in response to chan ging indust ry an d mar ket needs. All Uand many international specifications for LP-gas and othNGL products ar e based on t he work of this section.

Section F, Technical Data Deve lopment Monitors thstatus, availability, and reliability of thermodynamic aphysical property data needed for design and operation na tur al gas and gas processing facilities. This section idenfies indust ry needs for per tinent dat a, develops resear ch pr

jects t o provide needed data , and su pervises resear ch to methose needs. The section a lso evaluat es new corr elations ancompu ter models for calculation a nd application of ther modna mic and physical properties a pplicable to natu ral gas pr oessing and t ransport.

Pr imar y responsibility for initiation an d super vision of the

modynamic and physical properties research is vested in twsteering committees comprised of highly qualified and expeenced specialists. One committ ee directs resea rch int o ethalpy and heat tra nsfer, and th e second directs researinto phase behavior of gas liquids and related procest reams.

Section H, Product Measurement and HandlingMonitors measurement data and correlations for both natu rgas and n atu ral gas liquids, and r eviews han dling procedurfor gas liqu ids, includin g under ground st orage techn ology. Tsection initiates improvements in standards for accurameasurement and safe handling of both natu ral gas and gliquids.

Section L, Computer Technology and Data Distribtion - This Section is focused on two primary areas: 1) thcont inued development of the GPA Home Pa ge on th e Int ernan d; 2) the pusuit of data in sup port of the association and tactivities of the GPSA Editorial Review Board.

Section M, Operations an d Maintenance - This Sectiowas formed to assist member companies in addressing anresolving their operat ions an d main tenan ce issues, and to a forum where such issues on gas gathering and processincan be discussed. It is a nticipated th at the r esults of this committee can supplement the programs of the GPA regionMeetings.

GPS A TECHN ICAL ACTIVITIES

The Gas Processors Suppliers Association is an affiliatorganization of approximat ely 400 compan ies tha t cater to tsupply and service needs of the natural gas producing anprocessing indu str y. The prin cipal technical function of GPSis to publish GPA an d other t echnical inform ation thr ough tGPSA Engineering Data Book. In addition, technical experfrom GPSA compa nies pa rt icipat e in GPA techn ical comm ittactivities described above, and also provide valuable suppoan d counsel in directing therm odyna mic resear ch and techncal data development for the advancement of the industr ytechnology.

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Editorial Review Board The Editorial ReviewBoard for t he E ngineering Data Book is th e single GPSA tech-

nical comm itt ee. The Board is composed of recognized expert s

from both GPA an d GPSA member companies, an d is r espon-

sible for th e continu ing review and r evision of the E ngineering

Data Book to assure t hat it meets the n eeds of the natur al gas

processing industr y with th e latest dat a an d technology.

Definitions of Words and Terms Usedin the Gas Processing Industry

absorberA tower or column tha t pr ovides cont act between na tur al gasbeing processed an d a liquid solvent.

absorptionThe operation in which one or more components in the gasphase a re tr ansferr ed to (absorbed into) a liquid solvent.

absorption factorA factor which is an in dication of th e tende ncy for a given gasphase component t o be tran sferred to the liquid solvent. It isgenerally expressed as A = L/KV where L and V are t he m olesof liquid and vapor, and K is t he a verage value of the vapor-liquid equilibrium constant for the component of concern.

absorption oilA hydrocarbon liquid used to absorb and recover componentsfrom the nat ura l gas being processed.

acid gasThe hydrogen sulfide and/or carbon dioxide contained in, orextra cted from, gas or other str eams.

adiabatic expansionThe expan sion of a gas, vapor, or liquid str eam from a h igherpressu re to a lower pressur e in which th ere is no heat tr ansferbetween the gas, vapor, or liquid and t he sur roundings.

adsorbentA solid substa nce used to rem ove components from nat ura l gasbeing processed.

adsorptionThe process by which gaseous components are adsorbed onsolids because of their molecular attraction to the solid sur-face.

amine (alkanolamine)Any of several liquid compounds containing amino nitrogengenerally used in water solution to remove, by reversible

chemical reaction, hydrogen sulfide and/or carbon dioxide

from gas a nd liquid hydrocar bon st ream s.

API GravityAn arbitr ary scale expressing th e relat ive density of liquid pe-

tr oleum p roducts. The scale is calibrat ed in degrees API, cal-

culate d by the following formula :

Deg API =

141.5

Rel Den (15.56C/15.56C) 131.5

associated gasGaseous hydrocarbons occuring as a free-gas phase under

original oil-reservoir conditions of temperat ure an d pressu re.

atmospheric pressureThe pressur e exerted on the earth by the eart hs atm ospher e.

A pressur e of 760 mm of mercury or 101.3250 kPa is used a s

a standard for some measurements. State regulatory bodies

ha ve set other sta ndar ds for use in measur ing th e legal volume

of gas. Atmospheric pressure may also refer to the absolute

am bient pressur e at a ny given location.

barrel

A common English-unit measure of liquid volume which, inthe petroleum in dustr y, equals 42 U.S. liquid gallons for pe-

tr oleum or natu ra l gas liquid products measu red at 60F and

equilibrium vapor pressu re. One bar rel equals 0.159 cubic me-

ter s, or 6.29 barr els per cubic meter (SeeFig. 1-2).

blanket gasA gas pha se ma inta ined in a vessel contain ing liquid to pro-

tect the l iquid against air contam ination, to reduce th e haz-

ar d of detonat ion, or to maint ain pr essur e of th e liquid. The

source of the gas is exter na l to the vessel.

Components

CO2 H2S N2 C1 C2 C3 iC4 nC4 iC5 nC5 C6 C7+

Inert Gas

Acid Gas

LN G

Natural Gas

LP G

Natur al Gasoline

NGL

Condensa te (Stabilized)

FIG. 1-1

Typical Components of Industry Streams

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blow caseA sma ll tank in which liquid is accumu lated a nd t hen forcedfrom the tan k by applying as or air pressu re above th e liquidlevel.

blowdownThe act of emptying or depr essurin g a vessel. This ma y alsorefer to discarded material, such as blowdown water from aboiler or cooling tower.

boilaway testSometimes used to describe the GPA weather ing test for LP-gas. Refer to definition for "weathering test".

bottomsThe liquid or residual matter which is withdrawn from thebottom of a fractiona tor or other vessel during pr ocessing orwhile in storage.

B-P mixA liquefied hydrocar bon product composed chiefly of buta nesan d propane. If it originates in a r efinery, it m ay also conta inbut ylenes a nd pr opylene. More specifically, it conforms t o theGPA specifications for comm ercial B-P m ixes as d escribed inGPA Sta ndar d 2140.

breathingThe movement of vapor in or out of an at mospheric pressure

storage t ank becau se of a change of level of the stored liquid,a chan ge in th e tempera tur e of the vapor space above the liq-uid, or a change of at mospheric pressure.

bs&w (basic sedime nt and water)Waste tha t collects in th e bott om of vessels and tan ks conta in-ing petroleum or petr oleum pr oducts.

bubble pointThe temperatu re at a specified pressure at which the first st a-ble vapor form s a bove a liquid.

butane, commercialA liquefied hydrocarbon consisting predominately of butanean d/or bu tylene a nd wh ich conform s t o the GPA specificationfor comm ercial bu tan e defined in GPA Sta ndar d 2140.

butane, normalIn commer cial tr ans actions, a product meeting t he GPA speci-fications for commer cial but an e an d, in a ddition, conta ining aminimu m of 95 liquid volume percent n orm al buta ne. Chemi-cally, norma l buta ne is a n a liphat ic compound of the par affinseries ha ving the chemical form ula C4H10 an d ha ving all of itscarbon a toms joined in a str aight chain.

calorimeterAn appara tus which is used to determ ine the heat ing value ofa combust ible mat erial.

carbonyl su lfideA chemical compoun d of th e aldeh yde group cont ain ing a car -bonyl group and sulfur (COS). Sometimes a contaminant inna tur al gas and NGL. It ma y need to be removed in order tomeet sulfur s pecifications.

casinghead gasUnpr ocessed nat ura l gas produced from a reservoir containingoil. It conta ins hea vier hydrocarbon vapors a nd is usu ally pro-duced under low pressu re from a casing hea d on the well.

charcoal testA test stan dar dized by the Gas Pr ocessors Association and t heAmerican Gas Association for deter mining th e nat ur al gaso-line content of a given n atu ra l gas. The gasoline is adsorbedfrom the gas on a ctivated char coal and t hen r ecovered by dis-tillat ion. The test is pres cribed in Test ing Code 101-43, a jointpublication of AGA and GPA.

chromatographyA technique for sepa ra ting a mixtur e into individual compnents by repeated adsorption and desorption on a confinsolid bed. It is used for a na lysis of nat ura l gas and NGL.

Claus Proces sA process to convert h ydrogen sulfide into element al sulfur selective oxidat ion.

compress ibil ity factor

A factor, usu ally express ed as "Z," which gives the r at io of tactual volume of gas at a given temperature and pressure the volume of gas when calculated by the ideal gas la w.

compression ratioThe r atio of the a bsolute discharge press ure from a compr essto the absolute inta ke pressur e. Also applies to one cylindof a reciprocating compressor and one or more stages of a rtat ing compr essor.

condensateThe liquid formed by the condensation of a vapor or gas; spcifically, the hydrocarbon liquid sepa ra ted from n atu ral gbecau se of cha nges in tem perat ure an d pressur e when the gfrom the reser voir was delivered to th e surface separa tors. a steam system it may be water that is condensed and rtur ned to the boilers.

convergence pressureThe pressur e at a given tempera tur e for a hydrocarbon systeof fixed composition at which th e vapor-liquid equilibr ium Kvalues of the various components in the system become, tend to become, unity. The convergence pressure is used adjust vapor-liquid equilibrium K-values t o the par ticular sytem under consideration.

copper strip testA test u sing a sma ll strip of pure copper to determin e qualittively the hydrogen sulfide corrosivity of a product. Refer GPA LP-gas copper strip test (Copper Strip Method), ASTD-1838 test procedure.

cricondenbarThe highest pressure at which liquid and vapor phases ca

exist at equilibrium in a m ulticomponent system .cricondenthermThe highest tempera tur e at which liquid and vapor phases cexist at equilibrium in a m ulticomponent system .

PRESSURE

CONSTANTL

IQUID

%

CRIC

ONDENTHER

M

DEW

POINT

CRICONDENBAR

BUB

BLE

POINT

TEMPERATURE

CRITIC

AL

POINT

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crit ical densityThe density of a subst ance at its critical tempera tur e and criti-cal pressure.

crit ical pressureThe vapor pressure of a subst ance at its critical temper atu re.

crit ical temperatureFor a pure component, the m aximum temperat ure a t whichthe component can exist as a liquid.

cryogenic plantA gas pr ocessing plant which is capa ble of producing nat ur algas liquid products, including etha ne, at very low operatingtem perat ures, usu ally below minus 50C.

cubic meterA unit of volume m easur ement commonly used in interna tionalcommerce for petroleum, petroleum products and natural gas.One cubic meter measured at 15.56C = 264.172 U.S. gallons =6.29 barrels = 35.315 cubic feet measured at 15.56C.

deaeratorAn item of equipment used for rem oving air or other n on-con-densible gases from a pr ocess st ream or from st eam conden-sate or boiler feed water.

debutanizerA fractiona tor designed to separa te but ane (and more volatile

components if present) from a h ydrocarbon m ixtu re.

dehydrationThe a ct or process of removing water from gases or liquids.

demethanized productA product from which essentially all metha ne an d lighter ma -ter ials have been r emoved.

demethanizerA fractiona tor designed to separ ate m etha ne (and m ore vola-tile components if present) from a hydrocar bon m ixtu re.

depropanizerA fractionat or designed t o separat e propane (and more volatilecomponent s if present) from a hydrocarbon mixture.

desiccantA substa nce used in a dehydrat or to rem ove water a nd mois-tur e. Also a ma terial us ed to remove moisture from the air.

desulfurizationA process by which su lfur and sulfur compounds a re r emovedfrom gases or liquid hydrocarbon m ixtu res.

dew pointThe temperatu re at any given pressure, or the pressure at anygiven t empera tu re, at which liquid initially condenses from agas or vapor. It is specifically applied to the temper atu re atwhich water vapor starts to condense from a gas mixture(water dew point), or a t wh ich h ydrocar bons star t t o condense(hydrocarbon dew point).

distillationThe pr ocess of separat ing mat erials by successively heating tovaporize a portion and then cooling to liquefy a part of the

vapor. Mater ials to be separa ted mu st differ in boiling pointand/or relative volatility.

doctor testA qualitat ive method for det ecting h ydrogen sulfide and m er-captans in NGL. The test distinguishes between "sour" and"sweet" products.

dry gas(1) Gas whose water conten t ha s been reduced by a dehydra -tion pr ocess. (2) Gas cont ain ing little or no hydr ocar bons com-mercially recoverable as liquid product. Gas in this seconddefinition preferably should be called lean gas.

end pointThe maximum temperature observed on the thermometerduring a n ASTM distillation test.

EP-mix (ethane-propane m ix)A product consisting of a mixture of essentially ethane andpropane.

expansion turbineA device which convert s par t of the en ergy cont ent of a gas or

liquid str eam into mechanical work by expandin g the gas orliquid th rough a tu rbine from which work is extracted.

extractionThe pr ocess of tran sferring one or m ore components from oneliquid pha se to an oth er by virtue of different solubility in t hetwo liquids. It is also used to indicate re moval of one or moreconstituents from a stream.

f ield separatorA vessel in t he oil or gas field for separ at ing gas, hydr ocar bonliquid, and wa ter from each other.

f lash po intThe lowest temp era tur e at which vapors from a hydrocarbonliquid will ignite. Se e ASTM D-56.

fractionation

See definition of "distillation." Gener ally used to describesepar ation of a mixtur e of hydrocar bons into individual pr od-ucts based on difference in boiling point and/or relative vola-tility.

freeze valveA specially constructed and calibrated valve designed andused solely for determ ining the water content in pr opane prod-uct. See ASTM D-2713.

gas con stant (R)The constant multiplier in the Ideal Gas Law. Numerically,R=PV/T, if V is th e volum e of one mole of an ideal gas at tem -peratur e T and pressure P.

gas hydrateRefer to definition of "hydr at e".

gas injectionThe injection of natural gas into a reservoir to maintain orincrease th e reservoir pressur e or reduce the r at e of decline ofthe r eservoir pressure.

gas liftA method for bringing crude oil or water to the sur face by in-

jecting gas int o the pr oducing well bore.

gas-oil ratio (GOR)The ratio of gas to liquid hydrocarbon produced from a well.This may be expressed as standard cubic meters of gas percubic meter of stock tank liquid.

gas processingThe separation of constituents from natural gas for the pur-pose of mak ing salable products a nd also for trea ting th e resi-

due gas to meet required specifications.

gas processing plantA plant which pr ocesses na tur al gas for r ecovery of nat ura l gasliquids and somet imes other s ubsta nces such as sulfur.

gas-well gasThe gas pr oduced or sepa ra ted at surface conditions from thefull well stream produced from a gas r eservoir.

gas-well l iquidsThe liquid separa ted a t su rface conditions from th e full wellstr eam produced from a gas reser voir.

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gathering systemThe n etwork of pipelines which car ry gas from t he wells to theprocessing plant or other separ ation equipment.

heat media (heating media)A mat erial, whether flowing or st atic, used to tra nsport h eatfrom a pr imar y source such as combust ion of fuel to an otherma terial. Heatin g oil, steam , an d an eutectic salt mixtur e areexamples of heat media.

heating value (heat of combustion)The a mount of heat obtained by th e complete combust ion of aunit qu ant ity of mat erial. The gross, or h igher, hea ting valueis the amount of heat obtained when the water produced inth e combu stion is condens ed. The net , or lower, hea ting valueis the amount of heat obtained when the water produced inthe combust ion is not condensed.

heavy endsThe portion of a h ydrocar bon m ixtu re ha ving the highest boil-ing point. Usua lly hexanes or hept anes a nd all heavier hydro-carbons ar e the heavy ends in a n atur al gas stream.

hexane s plus (or heptanes plus)The portion of a hydrocar bon fluid mixtur e or th e last compo-nent of a hydr ocarbon a nalysis which contains t he hexan es (orhepta nes) and all hydrocar bons hea vier th an th e hexanes (or

heptanes).

hydrateA solid mat erial r esulting from t he combina tion of a hydrocar-bon with water un der pressure.

immiscibleLiquids tha t will not mix nor blend to give homogeneity ar esaid to be immiscible.

inertsElement s or compounds n ot acted upon chemically by the sur -rounding environment. Nitrogen and helium a re examples ofinert constituents of natural gases.

isobutaneIn commer cial tr ans actions, a product meeting t he GPA speci-

fication for commercial butane and, in addition, containing aminimu m of 95 liquid volume per cent isobuta ne. Chem ically,a h ydrocar bon of the par affin ser ies with t he formu la C4H10an d having its carbon atoms bran ched.

jacket waterWater which fills, or is circulated t hrough, a casing which pa r-tially or wholly sur rounds a vessel or m achine element in orderto remove, add, or distribute h eat in order to control the t em-pera tur e within t he vessel or element .

Joule-Thomson effectThe change in gas temper atu re which occur s when the gas isexpanded at constant enthalpy from a higher pressure to alower pressur e. The effect for m ost gases a t n orm al pressu re,except h ydrogen an d helium , is a cooling of th e gas.

lead acetate testA method for detecting the presence of hydrogen sulfide bydiscolora tion of paper which h as been moistened with lead ace-ta te s olut ion. See ASTM D-2420.

lean gas(1) The residue gas remaining after recovery of natural gasliquids in a gas pr ocessing plant . (2) Unpr ocessed gas contain-ing little or no recoverable na tur al gas liquids.

lean oilAbsorption oil as purchased or recovered by the plant, or oilfrom which t he absorbed const ituent s ha ve been r emoved.

lift gasGas used in a gas lift operation.

l ight endsThe low-boiling, easily evap orat ed componen ts of a hydrocabon liquid mixtur e.

l ight hydrocarbonsThe low molecular weight h ydrocarbons such as m etha ne, etane, propane an d butanes.

LNG (liquefied natu ral gas)The light hydrocar bon portion of na tur al gas, predominat emeth an e, which h as been liquefied.

loading rackA str uctur al an d piping insta llation a longside a ra ilroad tr aor roadway us ed for the p urpose of filling r ailroad ta nk caor tr ansport trucks.

LPG (liquefied petroleum gas )Refer t o definition of "LP-gas ".

LP-gas ( l iquefied petroleum gas)Pr edominat ely propane or butan e, either separ at ely or in mtures, which is maintained in a liquid state under pressuwithin the confining vessel.

LRG (liquefied refine ry gas)

Liquid propane or but ane produced by a crude oil refinery.may differ from LP-gas in that propylene and butylene mbe present.

LTX (low temperature extraction unit)A un it which uses t he cooling of a const an t ent ha lpy expan sito increase liquid r ecovery from st ream s pr oduced from higpressur e gas condensa te r eservoirs. Also called LTS (low t emperatur e separation) unit.

mercaptanAny of a homologous series of compounds of the general fomula RSH. All mer captans possess a foul odor.

miscible f loodA method of secondary recovery of fluids from a reservoir binjection of fluids tha t ar e miscible with th e reser voir fluid

natural gasGaseous form of petroleum. Consisting predominately of mitur es of hydrocarbon ga ses. The m ost comm on component methane.

natural gasolineA mixtur e of hydrocar bons, mostly pentanes and heavier, etracted from natural gas, which meets vapor pressure, enpoint, a nd other specifications for n atu ra l gasoline as adoptby the GPA. See GPA Sta nd ar d 3132.

natural gas processing plantTerm used for gas processing plant, natural gasoline plangasoline plant , etc.

NGL (natural gas liquid s)Natural gas liquids are those hydrocarbons liquefied at t

sur face in field facilities or in gas processing plant s. Natu rgas liquids include ethane, propane, butanes, and naturgasoline.

odorantAn odoriferous compoun d added to na tur al or LP-gas to impaa distinctive odor for detection of fugitive vapors. Ethyl mecaptan is the most widely used odorant for LP -gas, while tetiary butyl mercaptan, usually mixed with small amounts other compounds, is the predominan t odora nt for natu ra l ga

oil-well gasGas t hat is produced from an oil well.

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on-stream factorThe percentage of time a u nit is on-strea m.

operating factorThe percent age of time a un it is performing th e function forwhich it was designed.

outageThe vapor volume in a liquid vessel left for liquid expansion.Sometimes referred t o as ullage.

packaged unitA shop-assembled group of equipment and accessories whichneeds only foundations, inlet and outlet piping, and utilityconnections to make an opera ting unit.

packed columnA fractionation or absorption column filled with packing de-signed to give the r equired conta ct between the r ising vaporsan d th e descending liquid.

peak shavingThe u se of non-conventional fuels to supplement the n ormalsupply of pipeline gas during periods of extremely high de-mand.

pentane-plusA hydrocarbon mixture consisting of isopentane (C5H 12) and

heavier component s with higher boiling points.piggingA procedur e for forcing a device th rough a pipeline for clean ingpur poses, separa ting products, or inspecting the line.

pipeline gasGas which m eets a tra nsmission compa nys m inimum specifi-cations.

propaneA norm ally gaseous pa ra ffinic compound (C3H 8). The term in-cludes a ll pr oducts cover ed by GPA specifications for commer -cial a nd H D-5 propane. See GPA Sta ndar d 2140.

propane, commercialA liquefied hydrocarbon product consisting predominately ofpropane and/or propylene and which conforms to the GPA

specification for commer cial propan e as defined in GPA Sta nd -ar d 2140.

propane HD-5A special grade of propane consisting predominately of pro-pane and which conforms to the GPA specification for HD-5propane a s defined in GPA Sta nda rd 2140.

raw gasUnpr ocessed gas, or t he inlet gas t o a gas processing plant .

raw mix l iquidsA mixture of natural gas liquids prior to fractionation. Alsocalled "raw mak e".

recoveryThat percent or fraction of a given component in t he plan t feedwhich is r ecovered as plant product.

recycleReturn of part of a process stream to a point upstream fromwhere it was removed to enha nce recovery or contr ol.

refluxIn fractionat ion, th e port ion of condensed overhead r etur nedto the column to enhance achievable purity of the overheadproduct.

reflux ratioA way of giving a relat ive m easur ement to th e volume of reflux.Usua lly referr ed either t o the feed or overhead pr oduct.

relative densityThe ra tio of the ma ss of a given volume of a substan ce to tha tof another equ al volume of another s ubsta nce used as stan d-ard. Unless otherwise stated, air is used as t he stan dard forgases and water for liquids, with the volumes measured at15.56C an d a tmospheric pressur e (101.325 kPa ).

relief systemThe syst em for safely relieving excess pr essure to avoid ex-ceeding equipment design pressu re.

residueThe material which remains after a separation process. (1)Residue gas is tha t gas rema ining after th e recovery of liquidproducts. (2) Residue may also be the heaviest liquid or solidrem aining after distillat ion or r eclaiming process.

retrograde condens ation (vaporization)Condensa tion or va porization th at is the r everse of expectedbehavior. Condensa tion caused by a decrea se in pressu re or anincrease in tem perat ure. Vaporization caused by an increasein pressure or a decrease in temperature.

rich gasGas feed t o a gas processing plan t for liquid recovery.

rich oilThe oil leaving the bottom of an a bsorber. It is t he lean oil plus

the absorbed constituents.

RVP (Reid Vapor Pre ssu re)The vapor pressure of a material measured by the ReidMethod and apparatus as detailed in ASTM Test ProcedureD-323.

s & w (See bs&w)

saturated compoundsHydrocarbon compounds having no unsaturated carbon va-lence bonds. Natura l gas a nd nat ural gas liquids are sat urat edcompounds.

saturated l iquidLiquid which is a t its boiling point or is in equilibrium with avapor phase in its conta ining vessel.

saturated vaporVapor a t it s dew point.

shrinkageThe r eduction in volume of a gas st ream by removal of someof its constituents such as for recovered products, fuel, orlosses.

SNG (Synthetic or Substitute Natural Gas)The ga s pr oduct r esulting from t he gasification of coal and /orgas liquids or heavier h ydrocar bons.

solution gasGas which origina tes from t he liquid phas e in a n oil reservoir.

sourLiquids and gases ar e said t o be "sour" if th ey contain h ydro-gen sulfide, carbon dioxide, and/or mercaptans above a speci-

fied level. It also is used to refer to the feed stream to asweetening unit.

sour gasGas containing undesirable quantities of hydrogen sulfide,mer capt ans , and/or carbon dioxide. It also is used to refer tothe feed stream t o a sweetening unit.

splitterA nam e applied to fractiona tors, part icularly those separa tingisomers (e.g., butan e splitter refers t o a tower producing mostof the isobutan e in the feed as overh ead an d most of the n ormalbuta ne in th e feed as bottoms).

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sponge absorbentAn absorbent for recovering vapors of a lighter absorbent t ha tis used in the main absorption process of a gas processingplant.

stabilized condensateCondensa te tha t has been st abilized to a definite vapor pres-sur e in a fra ctionat ion system.

stabilizerA fractiona tion column designed t o reduce the vapor pressur eof a liquid stream .

stage separation systemA system of separators where the liquid portion of the welleffluent is separ ated from form ation gas and flash vapors.

stillThe column where t he absorbed product is recovered from t helean absorption oil. In plan ts u sing a low molecular weightabsorption oil, the still is designed as a fractionat ion column .In plants using a h igh m olecular weight absorption oil, the stillma y use steam or other fluids as stripping medium. Also usedto refer to regenerators in a mine tr eating an d glycol dehydra-tion system s.

strappingA term applied to the process of calibrating liquid storage ca-

pacity of storage tan ks in increment s of depth.stream dayA continuous 24 hour period of plant operation.

stripperA column wherein absorbed const ituent s ar e str ipped from th eabsorption oil. The ter m is applicable to column s using a str ip-ping medium, such as steam or gas.

stripping factorAn expression u sed t o describe th e degree of str ipping. Math e-ma tically, it is KV/L, th e reciprocal of the a bsorption fa ctor.

stripping mediumAs stated under "stripper", the medium may be steam, gas, orother m ater ial tha t will increase the dr iving force for s tripping.

sulfur

A yellow, non-met allic chemical element . In its element alsta te, it exists in both crystalline an d amorphous forms. Inma ny gas str eams, sulfur m ay be found a s volatile sulfur com-pounds, such as hydrogen su lfide, sulfur oxides, mercaptan s,an d car bonyl sulfide. Reduction of th e concentr at ion of th esegaseous su lfur compoun ds is often necessa ry for corr osion con-tr ol and p ossibly for hea lth a nd safety reasons.

sulfur dioxide (SO2)A hea vy, colorless , suffocating ga s t ha t is chemically an oxideof sulfur. Conversion of the gaseous sulfur oxides to sulfur isnecessary for corr osion contr ol, for hea lth a nd sa fety reasons,an d for complying with governm enta l stand ar ds.

sweetGas cont ainin g essent ially no objectionable su lfur compound s.Also, trea ted gas leaving a sweetening un it.

sweet gasGas which has n o more than the m aximum su lfur a nd/or CO2cont ent defined by (1) th e specifications for t he sa les gas froma pla nt ; (2) th e definition by a legal body. Also, the tr eat ed gasleaving a sweetening un it.

temperature correction factorA factor for corr ecting volume a t a given t empera tu re to th atat a specific reference temperature. Reference temperaturemost comm only used in the petroleum indus tr y is 15.56C.

thermA un it of gross h eat ing value e quivalent to (1.055) X 10

7kJ

tonneA unit of ma ss measu remen t, commonly used in intern ationpetroleum commerce; an expression for the metr ic ton, or 10kilograms.

trayed columnA vessel wher ein gas a nd liquid, or two par tia lly miscible l

uids, ar e conta cted, usua lly concurr ently on t rays. Also refto packed column.

turboexpanderRefer to definition of "expan sion tu rbin e."

ullage (See outage )

unsaturated compoundsHydrocarbon compounds ha ving one or m ore unsat ura ted vlence bonds, i.e., ethylene, propylene. These compounds anot found in n atu ra l gas str eams or gas liquids becau se of therelatively high chemical reactivity. Unsat ur ates ar e producby a th erma l cra cking or chemical r eaction an d can be founin synthetic gas (SNG) or light refinery gases (LRG).

vapor pressure (true vapor pressure)The pressu re exerted by the equilibrium vapor of a liquid wh

confined in a closed previously evacuat ed tan k or test appar atu

vapor pressure gasolineA descriptive phr ase for nat ura l gasoline meet ing a sp ecifivapor pressure.

vapor pres sure , GPAVapor pr essu re a s specified by GPA procedur es.

vapor recoveryEquipmen t or process for t he r ecovery of desired componenfrom stock t an k vapors or vapors from some other source.

volatile sulfurAn obsolete term referring to sulfur compounds t hat will vporize readily (See sulfur).

weathering

The evaporation of liquid caused by exposing it to the condtions of atm ospheric temper atu re an d pressure. Par tial evaprat ion of liquid by use of heat ma y also be called weath erin

weathering testA GPA test for LP-gas for the determination of heavy compnent s in a samp le by evapora tion under specified condition

weight in a irWeight compar ed to a stan dar d with n o corr ection for air bu oancy.

wellheadThe a ssembly of fittings, valves, and cont rols locat ed at thsurface and connected to the flow lines, tubing, and casing th e well so as t o contr ol th e flow from t he r eservoir.

wet gas(1) A gas conta ining water, or a gas which h as n ot been dehdra ted. (2) A term synonymous with r ich gas. Refer t o defintion of "rich gas".

Wobbe n umbe rA number proportional to the heat input to a burner at costa nt pr essure. In Br itish practice, it is the gross heating valof a gas divided by the squ ar e root of its gra vity. Widely usin Europe, together with a measured or calculated flamspeed, to determ ine inter changeability of fuel gases.

1-7


8/22

Conversion Factors

In t hes e ta bles, factors for conver sion, including conver sionsto the In ter nat iona l System of Units (SI), are based on ASTMStandard for Metric Practice, E380-91. The latest edition ofthis publication should be studied for more detail on the SIsystem, including definitions and symbols.

In calculat ing derived factors in th e tables t ha t follow, exactconversions were used, when available, rath er th an the 7-digitroun d-offs listed in ASTM E380 conversion ta bles. Derived fac-tors given below ar e rounded t o the sa me n umber of significan tdigits as t he source factors.

In an y conversion of funda ment al measu remen t un its, someconfusion may r esult du e to redefinition of units u sed in ear liertables. For example, in 1959 a sma ll refinement was ma de inthe definition of the yard, which changed its length from3600/3937 meter (or 1 inch = 25.4000508 mm) to 0.9144 mexactly (or 1 inch = 25.4 mm exactly). The tables below arebased on the new definition, but one should be aware thatwhere U.S. land measurements are concerned, the old rela-tionship applies. Refer to ASTM E380-91, note 13, for moredetail.

Similar confusion may arise in the definition of units forheat or ener gy. In t he ta bles below, the Btu (IT) an d calorie(IT) are used. These are the heat units recommended by theInternational Conference on the Properties of Steam, as de-fined:

1 Bt u (IT) = 1055.055 852 62 joule (exactly)1 Calorie (IT) = 4.186 800 joule (exactly)

For information only , other definitions tha t ma y be usedelsewhere:

1 Btu (Mean) = 1055.87 joule1 Bt u (39F) = 1059.67 joule1 Bt u (60F) = 1054.68 joule1 Btu (Therm ochem ical) = 1054.350 joule

1 calorie (Mean) = 4.190 02 joule1 calorie (15C) = 4.185 80 joule1 calorie (20C) = 4.181 90 joule1 calorie (Ther mochemical) = 4.184 000 joule

The funda ment al relationship between the Btu and the calo-rie:

grampound relationshipFahrenheit Celsius s cale r elationship

or: Btu 453.592 291.8

= calorie (IT, mean, or other)

Velocity(Length /unit of time)

ft /sec ft /min Miles/hr (U.S. Sta tu te) m/sec m/min km/hr

1 60 0.6818182 0.3048 18.288 1.09728

0.01666667 1 0.01136364 5.08 x 103

0.3048 0.018288

1.466667 88 1 0.44704 26.8224 1.609344

3.280840 196.8504 2.236936 1 60 3.6

0.05468066 3.280840 0.03728227 0.016667 1 0.06

0.9113444 54.68066 0.6213712 0.2777778 16.66667 1

Energy

Ft-lbf Kg-meter Btu (IT) Kilo-ca lorie (IT) Hp-hr Kilowat t -h r jou le (J )

1 0.1382550 1.285068 x 103

3.238316 x 104

5.050505 x 107

3.766161 x 107

1.355818

7.233014 1 9.294911 x 103

2.342278 x 103

3.653037 x 106

2.724070 x 106

9.806650

778.1692 107.5858 1 0.2519958 3.930148 x 104

2.930711 x 104

1055.056

3088.025 426.9348 3.968321 1 1.559609 x 103

1.163 x 103

4186.8

1980000 273744.8 2544.434 641.1865 1 0.7456999 2684520.

2655224 367097.8 3412.142 859.8452 1.341022 1 3600000.

0.7375621 0.1019716 9.478171 x 104

2.388459 x 104

3.725061 x 107

2.777778 x 107

1

FIG. 1-2

Conversion Factor Tables

1-8


9/22

Length

Inches Feet Yards Miles (U.S. Stat ut e) Millimet ers Meters

1 0.08333333 0.02777778 1.578283 x 105

25.4 0.0254

12 1 0.3333333 1.893939 x 104

304.8 0.3048

36 3 1 5.681818 x 104

914.4 0.9144

63360. 5280 1760 1 1609344 1609.3440 .0 39 37 00 8 3 .2 80 84 0 x 1 0

31.093613 x 10

36.213712 x 10

71 0.001

39.37008 3.280840 1.093613 6.213712 x 104

1000 1

Area

Sq inches Sq feet Sq yards Acres Sq miles (U.S. Sta tu te) Sq meters

1 6.944444 x 103

7.716049 x 104

1.594225 x 107

2.490977 x 101 0

6.4516 x 104

144 1 0.1111111 2.295684 x 105

3.587006 x 108

9.290304 x 102

1296 9 1 2.066116 x 104

3.228306 x 107

0.8361274

6272640. 43560. 4840. 1 0.0015625 4046.856

4014489600 27878400 3097600. 640 1 2589988.

1550.0031 10.76391 1.195990 2.471054 x 104

3.861022 x 107

1

Capacityvolume

Cu inches Cu feet Cu yards Liters Cu meters U.S. gallons Imp. gallons Barrels (42 U.S. gal)

1 5.787037 x 10 4

2.143347 x 105

0 .0 16 38 70 6 1 .6 38 70 6 x 1 05

4.329004 x 103

3.604649 x 103

1.030715 x 10 4

1728 1 0.03703704 28.31685 0.02831685 7.480520 6.228833 0.1781076

46656 27 1 764.5549 0.7645549 201.9740 168.1784 4.808905

61.02374 0.03531467 1.307951 x 103

1 0.001 0.2641720 0.2199692 6.289810 x 103

61023.74 35.31467 1.307951 1000 1 264.1720 219.9692 6.289810

231.0000 0.1336806 4.951132 x 103

3.785412 0.003785412 1 0.8326739 2.380952 x 102

277.4196 0.1605437 5.946064 x 103

4.546092 0.004546092 1.200950 1 0.02859406

9702.001 5.614584 0.2079475 158.9873 0.1589873 42 34.97230 1

Mass

Ounces Pounds Shor t tons Long tons Kilograms Metr ic t ons

1 0.0625 3.125 x 105

2.790179 x 105

0.02834952 2.834950 x 105

16 1 5 x 104

4.464286 x 104

0.4535924 4.535924 x 10 4

32000 2000 1 0.8928571 907.1847 0.9071847

35840 2240 1.12 1 1016.047 1.016047

35.27396 2.204623 1.102311 x 103

9.842065 x 104

1 0.00135273.96 2204.623 1.102311 0.9842065 1000 1

Weight per un it of area

Lb/sq ft Lb/sq in kg/sq cm kg/sq m Shor t tons/sq ft Long tons/sq ft kg/sq mm

1 0.006944444 4.882428 x 104

4.882428 0.0005 4.464286 x 104

4.882428 x 106

144 1 0.07030695 703.0695 0.072 0.06428571 7.030695 x 104

2048.161 14.22334 1 10000 1.024081 0.9143578 0.01

0.2048161 0.001422334 0.0001 1 1.024081 x 104

9.143578 x 105

0.000001

2000 13.88889 0.9764855 9764.855 1 0.8928571 0.009764855

2240 15.55556 1.093664 10936.64 1.12 1 0.01093664

204816.1 1422.334 100 1 000 000 102.4081 91.43578 1

Weight pe r unit of area , pressure

kgf/cm2

kPa lbf/in2

M m m e rcu r y (0 C ) i n. m er cu r y (3 2F ) i n. w a te r (3 9.2 F )atmospheres

(standard)

Millibars

1 98.06650 14.22334 735.561 28.9591 393.712 0.9678411 980.6650

0.01019716 1 0.1450377 7.50064 0.295301 4.01474 0.009869233 10

0.07030695 6.894757 1 51.7151 2.03603 27.6807 0.06804596 68.94757

0.00135951 0.133322 0.0193367 1 0.0393701 0.535253 0.00131579 1.33322

0.0345315 3.38638 0.491153 25.4 1 13.5954 0.0334210 33.8638

0.00253993 0.249082 0.0361263 1.86827 0.0735541 1 0.00245825 2.49082

1.033227 101.3250 14.69595 760.002 29.9213 406.794 1 1013.250

0.001019716 0.1 0.01450377 0.750064 0.0295301 0.401474 9.869233 x 104

1

FIG. 1-2 (Contd)

Conversion Factor Tables

1-9


10/22

A.P.I.

gravity

Baum

gravity

Specific

gravity

Lb/

U.S. gal

U.S. gal/

lb

kg/

Cu Meter

Cu

Meter/kg

0 10.2473 1.0760 8.9616 0.1116 1073.838 0.000931

1 9.2226 1.0679 8.8940 0.1124 1065.733 0.000938

2 8.1979 1.0599 8.8274 0.1133 1057.750 0.000945

3 7.1731 1.0520 8.7617 0.1141 1049.886 0.000952

4 6.1484 1.0443 8.6971 0.1150 1042.138 0.0009605 5.1237 1.0366 8.6333 0.1158 1034.503 0.000967

6 4.0989 1.0291 8.5706 0.1167 1026.979 0.000974

7 3.0742 1.0217 8.5087 0.1175 1019.564 0.000981

8 2.0495 1.0143 8.4477 0.1184 1012.256 0.000988

9 1.0247 1.0071 8.3876 0.1192 1005.051 0.000995

10 10.0000 1.0000 8.3283 0.1201 997.948 0.001002

11 10.9894 0.9930 8.2698 0.1209 990.945 0.001009

12 11.9788 0.9861 8.2122 0.1218 984.039 0.001016

13 12.9682 0.9792 8.1554 0.1226 977.229 0.001023

14 13.9576 0.9725 8.0993 0.1235 970.513 0.001030

15 14.9470 0.9659 8.0440 0.1243 963.888 0.001037

16 15.9364 0.9593 7.9895 0.1252 957.354 0.001045

17 16.9258 0.9529 7.9357 0.1260 950.907 0.001052

18 17.9152 0.9465 7.8826 0.1269 944.546 0.001059

19 18.9046 0.9402 7.8302 0.1277 938.270 0.001066

20 19.8940 0.9340 7.7786 0.1286 932.077 0.00107321 20.8834 0.9279 7.7276 0.1294 925.965 0.001080

22 21.8728 0.9218 7.6772 0.1303 919.933 0.001087

23 22.8622 0.9159 7.6275 0.1311 913.978 0.001094

24 23.8516 0.9100 7.5785 0.1320 908.101 0.001101

25 24.8410 0.9042 7.5300 0.1328 902.298 0.001108

26 25.8304 0.8984 7.4822 0.1336 896.569 0.001115

27 26.8198 0.8927 7.4350 0.1345 890.913 0.001122

28 27.8092 0.8871 7.3884 0.1353 885.327 0.001130

29 28.7986 0.8816 7.3424 0.1362 879.811 0.001137

30 29.7880 0.8762 7.2969 0.1370 874.363 0.001144

31 30.7774 0.8708 7.2520 0.1379 868.982 0.001151

32 31.7668 0.8654 7.2077 0.1387 863.668 0.001158

33 32.7562 0.8602 7.1638 0.1396 858.417 0.001165

34 33.7456 0.8550 7.1206 0.1404 853.231 0.001172

35 34.7350 0.8498 7.0778 0.1413 848.106 0.001179

36 35.7244 0.8448 7.0355 0.1421 843.043 0.00118637 36.7138 0.8398 6.9938 0.1430 838.039 0.001193

38 37.7032 0.8348 6.9525 0.1438 833.095 0.001200

39 38.6926 0.8299 6.9117 0.1447 828.209 0.001207

40 39.6820 0.8251 6.8714 0.1455 823.380 0.001215

41 40.6714 0.8203 6.8316 0.1464 818.607 0.001222

42 41.6608 0.8156 6.7922 0.1472 813.888 0.001229

43 42.6502 0.8109 6.7533 0.1481 809.224 0.001236

44 43.6396 0.8063 6.7148 0.1489 804.613 0.001243

45 44.6290 0.8017 6.6768 0.1498 800.055 0.001250

46 45.6184 0.7972 6.6392 0.1506 795.547 0.001257

47 46.6078 0.7927 6.6020 0.1515 791.090 0.001264

48 47.5972 0.7883 6.5652 0.1523 786.683 0.001271

49 48.5866 0.7839 6.5288 0.1532 782.325 0.001278

50 49.5760 0.7796 6.4928 0.1540 778.015 0.001285

A.P.I.

gravity

Baum

gravity

Specific

gravity

Lb/

U.S. gal

U.S. gal/

lb

kg/

Cu Meter

Cu

Meter/kg

51 50.5654 0.7753 6.4573 0.1549 773.751 0.001292

52 51.5548 0.7711 6.4221 0.1557 769.535 0.001299

53 52.5442 0.7669 6.3873 0.1566 765.364 0.001307

54 53.5336 0.7628 6.3528 0.1574 761.238 0.00131455 54.5230 0.7587 6.3188 0.1583 757.156 0.001321

56 55.5124 0.7547 6.2851 0.1591 753.118 0.001328

57 56.5018 0.7507 6.2517 0.1600 749.123 0.001335

58 57.4912 0.7467 6.2187 0.1608 745.170 0.001342

59 58.4806 0.7428 6.1861 0.1617 741.258 0.001349

60 59.4700 0.7389 6.1538 0.1625 737.387 0.001356

61 60.4594 0.7351 6.1218 0.1633 733.557 0.001363

62 61.4488 0.7313 6.0902 0.1642 729.766 0.001370

63 62.4382 0.7275 6.0589 0.1650 726.014 0.001377

64 63.4276 0.7238 6.0279 0.1659 722.300 0.001384

65 64.4170 0.7201 5.9972 0.1667 718.624 0.001392

66 65.4064 0.7165 5.9668 0.1676 714.986 0.001399

67 66.3958 0.7128 5.9368 0.1684 711.384 0.001406

68 67.3852 0.7093 5.9070 0.1693 707.818 0.001413

69 68.3746 0.7057 5.8776 0.1701 704.288 0.001420

70 69.3640 0.7022 5.8484 0.1710 700.792 0.00142771 70.3534 0.6988 5.8195 0.1718 697.332 0.001434

72 71.3428 0.6953 5.7909 0.1727 693.905 0.001441

73 72.3322 0.6919 5.7626 0.1735 690.512 0.001448

74 73.3216 0.6886 5.7346 0.1744 687.152 0.001455

75 74.3110 0.6852 5.7068 0.1752 683.824 0.001462

76 75.3004 0.6819 5.6793 0.1761 680.528 0.001469

77 76.2898 0.6787 5.6520 0.1769 677.265 0.001477

78 77.2792 0.6754 5.6251 0.1778 674.032 0.001484

79 78.2686 0.6722 5.5983 0.1786 670.830 0.001491

80 79.2580 0.6690 5.5719 0.1795 667.658 0.001498

81 80.2473 0.6659 5.5457 0.1803 664.516 0.001505

82 81.2367 0.6628 5.5197 0.1812 661.404 0.001512

83 82.2261 0.6597 5.4939 0.1820 658.320 0.001519

84 83.2155 0.6566 5.4685 0.1829 655.265 0.001526

85 84.2049 0.6536 5.4432 0.1837 652.239 0.001533

86 85.1943 0.6506 5.4182 0.1846 649.240 0.00154087 86.1837 0.6476 5.3934 0.1854 646.268 0.001547

88 87.1731 0.6446 5.3688 0.1863 643.324 0.001554

89 88.1625 0.6417 5.3445 0.1871 640.407 0.001562

90 89.1519 0.6388 5.3203 0.1880 637.515 0.001569

91 90.1413 0.6360 5.2964 0.1888 634.650 0.001576

92 91.1307 0.6331 5.2727 0.1897 631.811 0.001583

93 92.1201 0.6303 5.2492 0.1905 628.996 0.001590

94 93.1095 0.6275 5.2259 0.1914 626.207 0.001597

95 94.0989 0.6247 5.2029 0.1922 623.442 0.001604

96 95.0883 0.6220 5.1800 0.1930 620.702 0.001611

97 96.0777 0.6193 5.1573 0.1939 617.985 0.001618

98 97.0671 0.6166 5.1349 0.1947 615.293 0.001625

99 98.0565 0.6139 5.1126 0.1956 612.623 0.001632

100 99.0459 0.6112 5.0905 0.1964 609.977 0.001639

FIG. 1-3

A.P.I. and Baum Gravity Tables and Weight Factors

The relat ion of Degrees Baum or A.P.I. to Relative Density is expr essed byth e following formula s:

For liquids lighter than water:

Degrees Baum = 140 G

130, G =140

130 + Degrees Bau m

Degrees A.P.I. = 141.5G

131.5, G =141.5

131 .5 + Degrees A.P.I.For liquids heavier th an water :

Degrees Baum = 145 145

G, G =

145

145 +Degrees BaumG = Relative Dens ity = ra tio of the weight of a given volume of oil at 15.56C

to th e weight of the sam e volume of water a t 15.56C.

The above tables a re bas ed on the w eight of 1 U.S. gallon (3.785 liters ) ofoil with a volume of 231 cubic inches (3785 cubic centim eters) at 60F (15.56C)

in air a t 760 mm pre ssur e and 50% humidity. Assumed weight of 1 U.S. gallon

of water at 60F in air is 8.32828 pounds (3.77764 kg).

To determine t he resu lting gravity by mixing oils of different gra vities:

D =m d1+ nd 2

m + n

D = Densit y or Specific Gravity of mixtu re

m = Volume proport ion of oil of d1 density

n = Volume proport ion of oil of d2 density

d1 = Specific Gra vity of m oil

d2 = Specific Gra vity of n oil

1-10


11/22

Basis of units listed below is 22.4140 liters a t 0C and 1 at m for the volume of 1 g mole. All other va lues calculated from conversion factors listed in t ables.

n Temperatu re Pressure Volume R n Tempera t ure Energy R

gm mol K at m liter 0.082 057 477 gm mol K calor ie 1.985 9

gm mol K at m cm3

82.057 gm mol K joule 8.314 5

gm mol K mm H g liter 62.364

gm mol K bar liter 0.083 145 lb mol R Btu 1.985 9

gm mol K kg/cm2

liter 0.084 784 lb mol R hp-hr 0.000 780 48

gm mol K kPa m3

0.008 314 5 lb mol R Kw-hr 0.000 582 00

lb mol R at m ft3

0.730 24 lb mol R ft -lb 1 545.3

lb mol R in.H g ft3

21.850

lb mol R mm H g ft3

554.98 k mol K joule 8 314.5

lb mol R lb/in2

ft3

10.732

lb mol R lb/ft2

ft3

1 545.3

lb mol K at m ft3

1.3144

lb mol K mm H g ft3

998.97

k mol K kPa m3

8.3145

k mol K bar m3

0.083 145

FIG. 1-4

Values of the Gas Constant R in PV = nRT

Given base pr essure(See notes 1&2)

13.9 14.65101.325 kP a

@15C760 mm Hg

or 14.69614.696 @

59F14.7 14.73

14.73Sat.

30" Hg 14.9 15.025 16.4

13.9 1.0000 0.9488 0.9440 0.9458 0.9440 0.9456 0.9437 0.9603 0.9434 0.9329 0.9251 0.8476

14.65 1.0540 1.0000 0.9950 0.9969 0.9950 0.9966 0.9946 1.0122 0.9943 0.9832 0.9750 0.8933

101.325 kPa @15C 1.0593 1.0050 1.0000 1.0019 1.0000 1.0016 0.9996 1.0173 0.9993 0.9882 0.9800 0.8978

14.696 or 760 mm Hg 1.0573 1.0031 0.9981 1.0000 0.9981 0.9997 0.9977 1.0153 0.9974 0.9863 0.9781 0.8960

14.696 @59F 1.0593 1.0050 1.0000 1.0019 1.0000 1.0016 0.9996 1.0173 0.9993 0.9882 0.9800 0.8978

14.7 1.0576 1.0034 0.9984 1.0003 0.9984 1.0000 0.9980 1.0156 0.9976 0.9866 0.9784 0.8963

14.73 1.0597 1.0055 1.0004 1.0023 1.0004 1.0020 1.0000 1.0177 0.9997 0.9886 0.9804 0.8982

14.73 Sat . 1.0413 0.9880 0.9830 0.9849 0.9830 0.9846 0.9826 1.0000 0.9823 0.9714 0.9633 0.8826

30" Hg 1.0601 1.0058 1.0007 1.0026 1.0007 1.0024 1.0003 1.0180 1.0000 0.9889 0.9807 0.8984

14.9 1.0719 1.0171 1.0119 1.0139 1.0119 1.0136 1.0115 1.0294 1.0112 1.0000 0.9917 0.908515.025 1.0809 1.0256 1.0204 1.0224 1.0204 1.0221 1.0200 1.0381 1.0197 1.0084 1.0000 0.9162

16.4 1.1795 1.1195 1.1138 1.1159 1.1138 1.1156 1.1134 1.1331 1.1130 1.1007 1.0915 1.0000

Factor =Given Base Pr essure

Other Base Pressure

Other Base Temperatur e

Given Base TemperatureExa mp le: 14.65 to 14.73, 60F

14.65

14.73

459.67 + 60459.67 + 60

= 0.9946

FIG. 1-5

Commercial Base Pressure Conversion Factors

(Factors to Convert to Other Base Pressures)

psia in .Hg @ 32F mm H g @0C kPa

1 2.03603 51.7151 6.8948

0.491153 1 25.400 3.38638

0.019337 0.3937 1 0.1333

0.14504 0.2953 7.5006 1

13.9 28.3008 718.8399 95.83772

14.65 29.82784 757.62621 101.00882

14.696 29.9215 760.0051 101.32598

14.6959 29.9213 760.00 101.3250

14.7 29.9296 760.21197 101.3536

14.73 29.9907 761.7634 101.5604

14.73456 30.00 761.999 101.5918

14.9 30.3368 770.55499 102.73252

15.025 30.59135 777.01937 103.5944

16.4 33.39532 848.12764 113.0747

FIG. 1-6

Pressure Equivalents

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Kin ema t ic viscosity(centistokes) =absolute viscosity (centipoises )

density (g/cm 3)

ft2/se c = (centistokes)(1.07639 10 5)

centistokes = (ft2/se c)(92903.4)* Usua lly same a s specific gravity.

APPROXIMATE VISCOSITY CONVERSIONS

ft2/sec (50100SSU ) = [(SS U)(2.433 10 6)](0.00210 /SS U)

ft2/sec(10 0350 SSU) = [(SS U)(2.368 10 6)] (0.00145/SS U)

ft2/sec (over 350 SSU ) = [SSU (at 100F )(2.3210 10 6)]

centistokes (5010 0 SS U) = [(SSU)(0.226)](205.3/SS U)centistokes (10 0350 SSU) = [(SSU)(0.220)] (147.7/SS U)centistokes (over 350 SSU) = [SSU(a t 100F or 37.8C)(0.21576)]centistokes (over 350 SSU) = [SSU(a t 210F or 98.9C)(0.21426)]centistokes (over 500 SSU) = [SSU (at 122F or 50C)(2.120 )]

centistokes (over 300 Redwood #1) = [Redwood #1 (S t a n d a r d)(0.255)]centis tokes (over 50 Redwood #2) = [Redwood #2 (Admiralty)(2.3392)]

centistokes (over 18 E ngler) = (Engler )(7.389)

centistokes (over 20 Storm er) = (Stormer)(2.802)centistokes (over 1.0 Demler #1 0) = (Demler #10)(31.506)

centistokes (over 1.3 Demler #1) = (Demler #1)(3.151)centistokes(over 14 Pa rlin #20) = (Par lin Cup #2 0)(61.652)

centistokes (over 230 Ford #4) = (Ford Cup #4)(3.753)cen t is tokes = 6200 Barbey

VISCOSITY UNIT CONVERSIONS

KINEMATIC VISCOSITY

MULTIPLY BY TO OBTAIN

ft2/sec 92903.04 cen t istokes

ft2/sec 0.092903 sq meter s/sec

sq m eter s/sec 10.7639 ft2/sec

sq meters/sec 1 000 000.0 cent istokes

cent istokes 0.000 001 sq meter s/sec

cent istokes 0.000 010 763 9 ft 2/sec

ABSOLUTE OR D YNAMIC VISCOSITY

lbf-sec/ft2

47880.26 cent ipoises

lbf-sec/ft2

47.8803 Pasca l-sec

cent ipoises 0.000 102 kg-sec/sq m eter

cent ipoises 0.000 020 885 4 lbf-sec/sq ft*

cent ipoises 0.001 Pasca l-sec

Pasca l-sec 0.020 885 4 lbf-sec/sq ft

Pasca l-sec 1000 cen tipoises

* Sometimes absolute viscosity is given in terms of pounds ma ss. In th is case (centipoises)(0.000672) = lbm /ft sec.

ABSOLUTE TO KINEMATIC VISCOSITY

cent ipoises 1/density (g/cm3) cent istokes

cent ipoises 0.000 671 97/density (lb/ft3) ft

2/sec

lbf-sec/ft2 32.174/den sity (lb/ft3) ft 2/sec

kg-sec/m2

9.80665/density (kg/m3) sq m eters/sec

Pasca l-sec 1000/density (g/cm3) cent istokes

KINEMATIC TO ABSOLUTE VISCOSITY

cent istokes den sity (g/cm3) cent ipoises

sq meters/sec (0.10197)[density (kg/m3)] kg-sec/sq m eter

ft2/sec (0.03108) [density (lb/ft

3)] lbf-sec/ft

2

ft2/sec (1488.16) [density (lb/ft

3)] cen t ipoises

cent istokes (0.001) [density (g/cm3)] Pasca l-sec

sq m eter s/sec (1000) [density (g/cm3)] Pasca l-sec

FIG. 1-7

Viscosity Relationships

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Other useful relationships:

1 Therm ochemical un it x 0.999 331 2 = IT Un it (Btu orother)

1 Ther mochemical cal/gm x 1.8 x 0.999 331 2 = IT Btu /lb

Ent ropy, 1 Btu /(lb R) = 4.186 8 kJ/(kg K)

Ent halpy, 1 Btu/lb = 2.326 kJ/kg

1 Gra in = 64.798 91 mg

1 Gra in/100 scf = 22.888 352 mg/m3

1 Gra in/U.S. gallon = 1 7.118 06 g/m 3

C = 5/9 (F 32)

F = 9/5 (C)+ 32

K = C + 273.15 = 5/9 R

R = F + 459.67 = 1.8 K

1 newt on of force = 1 kg m/s2 = 1 N

1 pascal pressu re = 1 N/m2 = 1 Pa

Notes:

1. Pressure is stated as psia except where specifically indcated other wise.

2. Base temperature is assumed to be 60F except whespecifically indicat ed other wise.

3. Satur ated water vapor pressure at 60F equals 0.25psi (Intern ational Cr itical Tables).

4. 60F = 15.6C 15C = 59F

5. 30" Hg @32F is normally assu med equivalent to 14.psi commercially.

6. To convert h eatin g value or gas price from one base pr esure to another, the reciprocals of the above conversiofactors a pply.

7. kPa represents kPa (abs) unless indicated as kP a (ga) fgauge pressure.

8 . kJ/(kmol K) = kJ /(kmol C)

GPA Publications*TECHNICAL STANDARDS MANUAL A one-volume

loose-leaf manual that contains the official test methodsan d specifications of th e GPA. Included ar e GPA Sta nda rds101-43, 2140, 2142, 2145, 2165, 2166, 2172, 2174, 2177,2186, 2187, 2188, 2194, 2261, 2265, 2286, 2377, 3132, 8173,8182, 8186, 8195, RB-181, RB-194 an d ASTM Test P roce-dur es D86, D130, D156, D216, D287, D323, D1070, D1265,D1267, D1657, D1837, D1838, D2158, D2163, D2713,D2784. Subject tabbed for ready reference.

PLANT OPERATIONS TEST MANUAL A one-volumeloose leaf ma nua l conta ining the significant tests comm onlyused in the opera tion of a plant. Th is convenient compila-

tion contains test methods which originated with ASTM,API, PEA, GPA, U.S. Bureau of Mines, Betz Laboratories,Girdler Corp. and Fluor Corporation. In addition, it con-tains all of the information in the "Technical StandardsManual."

CORROSION DETECTION REPORT A practical andconvenient field guide t o detecting, locating, and measu ringcomm on corr osion p roblems in gas processing plant s a ndrelated equipment.

PLANT PROJECT AND DESIGN CHECK LIST Pre-par ed by Technical Section A to serve as a guide in pla nn ingan d prepa ring job and equipment s pecifications using cate-gories norm ally required for a pr ocessing plant .

EN ERGY CONSE RVATION CHECK LIST Prepared byTechnical Section A, and pa tter ned after the ea rlier "PlantProject and Design Check List", it was developed to serveas a guide check list for energy conservat ion with in var iousunits of equipment .

SAFETY INSP ECTION CHECK LIST Prepared by theSafety Committee to show the plant and design engineeritems of importance to check from the viewpoint of safetyin design and operation. It consists of approximately 60pages covering 15 areas in th e gas processing plant .

GUIDE FOR PERFORMANCE TESTING OF PLANEQUIPMENT Prepared by Section A as a guide fchecking the performance of various items of equipmewithin a plant. Over 200 pages divided into five major setions: A. Pla nt Accept an ce an d Per form an ce Tests ; B. Toers an d Vessels; C. Engines a nd Turbines; D. Compr essoPu mps an d Blowers; and E. Heatin g and Cooling.

BIBLIOGRAPHY ON HYDROCARBONS A comp reh esive bibliograph y of importa nt art icles on hydrocar bons anassociat ed compounds. Over 100 pages with 1300 abstr accloth bound, 9 x 12 inches. The text material covers thperiod from 1946-1960 inclusive. It contains a wealth

time-saving references for petroleum en gineers, chemistresear chers, a nd st udent s. J . A. Muckleroy.

NORTH AMERICAN STORAGE CAPACITY FOR LIGHHYDROCARBONS AND U.S. LP -GAS IMPORT TEMINALS A biennia l report compiling th e stora ge facities for light hydrocarbons in the U.S. and the terminfacilities in the U.S. capable of receiving imported LP-gaLotus 123 Diskette a vailable.

SALES OF N ATURAL GAS LIQUIDS AND LIQUEFIEREFINERY GASES A joint publicat ion of API, GPand NPGA summarizes annual survey data on gas liquisales by product, by major mar ket u ses, and by stat e.

NGL SU P P LY/DE MAND/INVENTORY DATA A comp

lation of historical gas plant and refinery production of gliquids pr oduction, by month a nd by product. Data are etended t o include total monthly supply, demand and invetories of individua l products . Also availa ble on LOTUS 1diskette. Current monthly summaries of these data aavailable on r equest.

LP-GAS ODORIZATION SYMPOSIA PROCEEDINGSCollection of paper s pr esented a t t wo symposia on LP -gOdorizat ion Technology in 1989 a nd 1 990. Co-sponsored bthe Na tional Propane Gas Association and th e Propane GAssociation of Canada, these proceedings are a thoroug

1-13


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compilat ion of informa tion on LP-gas odoran ts, odoriza tionpra ctices and equipmen t, and origina l research into the be-ha vior of odora nts in the LP -gas fuel system .

REPORT OF INVESTIGATIONSODORIZATION OFLP-GAS A summary of research findings and studiesconducted during 1986-1990 by a joint task force of repre-senta tives from GPA, th e Nat iona l Pr opan e Gas Associationan d the P ropane Gas Association of Can ada . Includes t askforce r ecomm enda tions for effective odorization of LP-gas.

ANNUAL CONVENTION P ROCEEDINGS Collection ofall technical papers pr esented in the t echnical forum s an dgeneral sessions of the GPA an nua l conventions.

Standards and Bulletins

Specif ications

GPA Standard 2140 Liquefied Petroleum Gas Specifica-tions an d Test Meth ods.

GPA Standard 3132 Natu ral Gasoline Specifications a ndTest Methods.

Analytical Methods

AGA-GPA CODE 101 Standard Compression a nd Char -coal Tests for Determining th e Nat ura l Gasoline Cont ent ofNatural Gas.

GPA Stand ard 2165 Standa rd for Ana lysis of Nat ura l GasLiquid Mixtur es by Gas Chr omatography.

GPA Stan dard 2177 Analysis of Demetha nized Hydrocar -bon Liquid Mixtu res Conta ining Nitrogen and Ca rbon Di-oxide by Gas Chromatography.

GPA Standard 2186 Tenta tive Method for th e ExtendedAnalysis of Hydrocarbon Liquid Mixtures Containing Ni-

trogen and Carbon Dioxide by Temperature ProgrammedGas Chr oma tography.

GPA Sta nda rd 2187 Tenta tive Method for the Determ ina-tion of Ammonia in Liquid Pr opan e.

GPA Sta nda rd 2l88 Tenta tive Method for the Determina -tion of Ethyl Mercaptan in LP-gas Using Length of StainTubes.

GPA Standard 2194 Low Pressure Field Method for De-termining Ethyl-Mercaptan Odorant in LP-Gas UsingLength of Stain Tubes.

GPA Stan dard 2261 Analysis for Na tur al Gas an d SimilarGaseous Mixtur es by Gas Chr omatography.

GPA Standard 2265 GPA Sta ndar d for Deter mina tion ofHydrogen Sulfide and Mercaptan Sulfur in Natural Gas(Cadmium Sulfate-Iodometric Titrat ion Method).

GPA Stand ard 2286 Tent at ive Meth od of Extend ed Ana ly-sis for Natu ra l Gas and Similar Ga seous Mixtures by Tem-peratur e Pr ogramm ed Gas Chromatography.

GPA Sta nda rd 2290 Tenta tive Method for the Determ ina-tion of Carbonyl Sulfide (COS) in Unodorized Liquid Pro-pane.

GPA Stan dard 2377 Test for Hydr ogen Su lfide an d Car bonDioxide in Na tur al Gas Using Length of Stain Tubes.

Measurement Standards

GPA Stan dard 2142 Stan dar d Fa ctors for Volume Corr ec-tion and Specific Gravity Conversion of Liquefied Petro-leum Gases.

GPA Stand ard 2145 Physical Constant s for P ar affin Hy-drocarbons and Other Components of Natural Gas. Dataare given in both English an d SI U nits. Revised yearly.

GPA Stand ard 2172 Calculation of Gross Heating Value,Specific Gravity and Compressibility of Natural Gas Mix-tur es from Compositional Analysis.

GPA Stan dard 8173 Method for Converting Mass Na tur alGas Liquids and Vapors to Equivalent Liquid Volumes.Data a re given in both E nglish and SI Units.

GPA Standard 8182 Tentative Standard for the MassMeasurement of Natural Gas Liquids.

GPA Stan dard 8186 Measurem ent of Liquid H ydrocar bon

by Tru ck Scales.GPA Standard 8195 Tentative Standard for Converting

Net Vapor Spa ce Volumes t o Equivalen t Liqu id Volumes.

GPA Referen ce B ulletin 181 Heat ing Value a s a Bas is forCustody Transfer of Natural Gas. A reference to provideau thoritat ive interp reta tion of accepted procedur es for de-termining heating values.

GPA Reference Bulletin 184 Tentative NGL LoadingPractices

GPA Stan dard 8185 Orifice Metering of Nat ura l Gas an dOther Related Hydrocarbon Fluids. This is t he 1985 versionof AGA #3, now issu ed a s API /ANSI 2530 an d GPA 8l85. Thelatest edition of this publication is being pu blished in four

par ts an d is available from API.

Sampling Methods

GPA Standard 2166 Obtaining Natural Gas Samples forAna lysis by Gas Chromat ograph y.

GPA Stan dard 2174 Meth od for Obtain ing Liquid Hydro-carbon Sam ples Using A Floatin g Piston Cylinder.

Miscel laneou s Standards

GPA Publication 1167 GPA Glossa ry-Definit ion of Wordsand Terms Used in t he Gas P rocessing Indust ry.

* GPA Committees periodically update or revise GPA publica-tions. The last two digits of the year in which the publicationis revised are appended to the publication number, e.g., GPA

2145-93.

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GPA Research Reports

Result s of most of the GPA sponsored r esear ch projects sin ce1971 have been published as n umber ed Research Reports. Insome cases, individual compan y sponsored dat a ha ve beenpublished a s Technical Pu blications.

RR-1 Bibliography of Data Sources for Low-TemperatureVapor-Liquid Equilibria in Non-Absorber Oil Sys-tems R. D. Gunn a nd S . V. Mainka r, Universityof Texas, Austin, Texas. Project 692-A.

RR-2 K-Values in Highly Aromatic and HighlyNaphthenic Real Oil Absorber Systems - Grant Wil-son and Sherman T. Barton, P-V-T, Inc., Houston,Texas. P roject 691.

RR-3 Enthalpy and Entropy of Non-Polar Liquids at LowTemperatures - K. C. Chao and R. A. Greenkorn,Pu rdu e University, Lafayette, Indiana .

RR-4 Evaluation of Eight Enthalpy Correlations - Ken-neth E. Starling, David W. Johnson and Philip C.Colver, University of Oklahoma, Norman, Okla-homa. P roject 68l.

RR-5 Experimental Measurements of Vapor-Liquid Equilib-rium Data for the Ethane-Carbon Dioxide and Nitro-

gen-n-Pentane Binary Systems - Kurata-SwiftConsulting Engineers, Lawrence, Kansas. Project692-B.

RR-6 Enthalpies of Methane-C7 Systems - Bert Eakin,Grant M. Wilson and Will E. DeVaney, P-V-T, Inc.,Houst on, Texas. P roject 661.

RR-7 The Equilibrium Phase Properties of the Binary Sys-tems: Nitrogen-Hydrogen Sulfide, Isobutane-Hydro-

gen Sulfide, Isobutane-Carbon Dioxide andIsobutane-Ethane - D. B. Robinson a nd G. J . Besserer,Univers ity of Albert a, Edmonton, Alberta .

RR-8 1971-1972 Enthalpy Correlation Evaluation Study- Kenneth E. Starling, University of Oklahoma,Norma n, Oklahoma. P roject 713.

RR-9 Enthalpies of Hydrogen Sulfide-Methane-EthaneSystems - Bert Eakin and Will E. DeVaney, P-V-T,In c., Houst on, Texas. P roject 722.

RR-10 Solubility of Solid Carbon Dioxide in Pure Light Hydrocarbons and Mixtures of Light Hydrocar-bons - Fred Kurata, Center for Research, Inc.,Lawrence, Kansas.

RR-11 GPA Experimental Enthalpy Values Referred to TwoBase Levels - John M. Lenoir a nd Gene A. Cochran,

University of Southern California, Los Angeles,California. Project 733.

RR-12 Enthalpy and Phase Boundary Measurements onCarbon Dioxide and Mixtures of Carbon Dioxidewith Methane, Ethane and Hydrogen Sulfide -Gran t M. Wilson an d J ames M. Peter son, BrighamYoung Un iversit y, Pr ovo, Uta h. P roject 731.

RR-13 Prediction of Absorber Oil K-Values and Enthalpies- John H . Erbar, Oklahoma St ate Un iversity, Still-water, Oklahoma. P roject 714.

RR-14 Solubility of Heavier Hydrocarbons in Liquid Metane - Fred Kurata, Center For Research, IncLawrence, Kansas. Project 738-A.

RR-15 The Equilibrium Phase Properties of Selected Bnary Systems at Low Temperature: Nitrogen-Hdrogen Sulfide, Ethane-Hydrogen Sulfide ann-Butane-Carbon Dioxide - D. B. Robinson and Kalra, University of Alberta, Edmonton, AlbertProject 738.

RR-16 Solubility Limits of Heavy Hydrocarbons in NGand LNG Mixtures - Will DeVan ey, Bert Ea kin a nJames M. Berryman, P-V-T, Inc., Houston, TexaPr oject 735-A.

RR-17 Smoothed Experimental Enthalpy Data for ThrMethane-Ethane Binaries and a Methane-EthanPropane Ternary - J ohn E. P owers, Andre W. Futad o, Ravi Kant a nd Adriana Kwan , UniversityMichigan , Ann Arbor, Michigan. P roject 723.

RR-18 The Equilibrium Phase Properties of Selected B

nary Systems: n-Heptane-Hydrogen Sulfide, Heptane-Carbon Dioxide and i-Butane-NitrogenD. B. Robinson and H . Kalra, Un iversity of AlbertEdm onton, Alberta. P roject 745.

RR-19 Vapor Phase Data for the Binary Systems of Metane with n-Butane, n-Pentane, n-Hexane and

Heptane - Roger J. J. Chen, Patsy S. Chappeleand Riki Kobayashi, Rice University, HoustoTexas. Pr oject 692-B.

RR-20 K-Values for the Methane-n-Butane, MethanePentane and Methane-n-Hexane Systems - Doug Eliot, Y. N. Lin, T. C. Chu, Pa tsy S. Ch appelea r a nRiki Kobayashi, Rice University, Houston, TexaPr oject 692-B.

RR-21 Dew-Point Values for the Methane-Carbon DioxiSystem - S. C. Hwang, Ho-Mu Lin, Pa tsy S. Chapelear and Riki Kobayashi, Rice University, Houton, Texas. P roject 7 39.

RR-22 Solubility of Hydrocarbons in Cryogenic LNG an NGL Mixtures - James P. Kohn and Kraemer Luks, University of Notre Dame, Notre Dam e, Idiana . Pr oject 735.

RR-23 Measurement of Ethane and Propane Recovery anTotal Fraction Condensed for Simulated NaturGas Mixtures - Grant M. Wilson, J ohn R. Cunninha m, B. Steve Lofgren a nd Veldon E. Messick, Themochemical Inst itu te, Brigha m Young Universi

Provo, Utah. Project 737.

RR-24 Enthalpy and Phase Boundary Measurements Mixtures of Nitrogen with Methane, Carbon Dioxidand Hydrogen Sulfide - Grant M. Wilson, J ohn Cunnin gham an d Pa ul F. Nielsen, Brigham YouUniversity, Provo, Utah. Project 741.

RR-25 The Vapor-Liquid Equilibrium of the CH4-CO2 Sytem at Low Temperatures - S. C. Mraw, S. C. Hwanand Riki Kobayashi, Rice University, HoustoTexas. P roject 739.

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RR-26 Statistical Thermodynamics of Solutions in Natu-ral Gas and Petroleum Refining - M. D. Donohueand J. M. Prausnitz, University of California,Berke ley, Californ ia. P roject 721.

RR-27 Solubility of Hydrocarbons in Cryogenic LNG and NGL Mixtures - James P. Kohn and Kraemer D.Luks, University of Notre Dame, Notre Dam e, In-dian a. Pr oject 735-A.

RR-28 The Characterization of the Heptanes and HeavierFractions for the GPA Peng-Robinson Programs - D.B. Robinson an d D. Y. Pen g, Universit y of Alber ta ,Edm onton, Alberta. Project 756.

RR-29 The Equilibrium Phase Compositions of Selected Aromatic and Naphthenic Binary Systems: Tolu- ene-Carbon Dioxide, Toluene-Hydrogen Sulfide, Methylcyclohexane-Carbon Dioxide and Methylcy-clohexane-Hydrogen Sulfide - D. B. Robinson andH-J Ng, University of Alberta, Edmonton, Alberta .Pr oject 755, 755-A and 757-B.

RR-30 High Temperature V-L-E Measurements for Substi-tute Gas Components - Will DeVan ey, J am es M. Ber -ryman, Pen-Li Kao and Bert Eakin, P-V-T, Inc.,

Houst on, Texas. P roject 757.

RR-31 The Equilibrium Phase Properties of a SyntheticSour Gas Mixture and a Simulated Natural Gas

Mixture - D. B. Robinson, H. Kalra and H an s Rem-pis, University of Alberta, Edmonton, Alberta. Pro-

ject 737-A & 737-B.

RR-32 Vapor-Liquid Compositions of Propane-ButaneMixtures in Cold Weather Field Tests - Thomas H.May and Dorab N. Bar ia, University of North Da-kota, Gran d Forks, Nort h Dakota. P roject 789-A.

RR-33 Solubility of Hydrocarbons in Cryogenic LNG and NGL Mixtures - James P. Kohn and Kraemer D.Luks, University of Notre Dame, Notre Dam e, In-

diana . Pr oject 735.RR-34 Sour Water Equilibria: Ammonia Volatility Down

to ppm; Effect of Electrolytes on Ammonia Volatility; pH vs. Composition - Grant Wilson, Richard S.Owens and Marshall W. Roe, Wilco Research,Pr ovo, Utah . Pr oject 758-A.

RR-35 Computer Simulations of Vapor-Liquid Composi-tions of Propane-Butane Mixtures in Cold Weather

Field Tests - Thomas H. May and Dorab N. Baria,University of North Dakota, Grand Forks, NorthDakota. Project 789-B.

RR-36 Literature Survey for Synthetic Gas Components--Thermodynamic Properties - P. Pender graft , M. Mar -ston, M. Gonzales, V. Rice and J . Erbar, Oklahoma

State University, Stillwater, Oklahoma. Project 746.

RR-37 Enthalpy Measurements on Synthetic Gas Systems: Hydrogen-Methane, Hydrogen-Carbon Monoxide -James M. Berryman, Will E. DeVaney, Bert E.Eakin and Nancy L. Bailey, P-V-T, Inc., Houston,Texas. P roject 742.

RR-38 A Preliminary Version of the PHC Equation of StateComputerized for Engineering Calculations - E. C.Hohman n, Californ ia St at e P olytechnic University,Pomona, California. Project 771.

RR-39 The Equilibrium Phase Properties of Selected m- Xylene and Mesitylene Binary Systems: CH2-m- Xylene, CO2-m-Xylene, CH4-Mesitylene - D. B.Robinson, H-J Ng and S-S Hu an g, Un iversity of Al-berta , Edm onton, Alberta . Pr oject 755-B.

RR-40 Measurement of Ethane and Propane Recovery andTotal Fraction Condensed in the Bubble Point Re-

gion of Two Simulated Natural Gas Mixtures - JohnR. Cunningham, John L. Oscarson and Mark L.J ens on, Brigha m Young Univer sity, Provo, Utah .Project 737.

RR-40A Phase Equilibria of a High Nitrogen Content Syn-thetic Natural Gas - Ja mes P. Kohn a nd Robert C.Merrill, University of Notre Dame, Notre Dam e, In-diana . Pr oject 795.

RR-4l Vapor-Liquid Equilibrium Data on Water-Substi-tute Gas Components: N2-H2O, H2-H2O, CO-H2Oand H2-CO-H2O and H2S-H2O - Paul C. Gillespiean d Gra nt Wilson, Wilco Resea rch Co., Pr ovo, Uta h.Pr oject 758-B.

RR-42 Predicting Synthetic Gas and Natural Gas Thermody-namic Properties Using a Modified Soave Redlich

Kwong Equation of State - J. H. E rbar, A. K. Jagota,S. Muthswam y and M. Moshfeghian, Oklahoma St ateUniversit y, Stillwater, Oklahoma . Pr oject 752.

RR-43 The Equilibrium Phase Properties of Selected m-Xylene and Mesitylene Binary Systems: m-Xylene-Mesitylene-H2S, Mesitylene-CO2 - D. B. Robinsonan d S-S Hua ng, University of Alberta, E dmonton,Albert a. P roject 755-B.

RR-44 Vapor-Liquid and Liquid-Liquid Equilibria in the Methane-Toluene System and Relation of Liquid-Liquid Equilibrium Behavior at Low Temperaturesto Vapor-Liquid Equilibria Behavior at High Tem-

peratures and Elevated Pressures - Yeuh -Neu Lin ,Shuen -Cheng Swan g and Riki Kobayashi, Rice Uni-

vers ity, Houst on, Scott W. Hopke, Exxon P roductionCompan y, Houst on, Texas. P roject 757.

RR-45 The Water Content and Correlation of the WaterContent of Methane in Equilibrium with Hydrates,(I); and the Water Content of a High Carbon DioxideSimulated Prudhoe Bay Gas in Equilibrium with

Hydrates, (II) - Keichi Aoyagi, Kyoo Y. Song an d Rik iKobayashi, Rice University, Houston, Texas, E.Dendy Sloan a nd P. B. Dha rm awar dhan a, Dept. ofChemical Engineering, Colorado School of Mines,Golden, Colora do. Pr oject 775.

RR-46 Vapor Liquid Equilibrium Study of the H2-CH4 Sys-tem at Low Temperatures and Elevated Pressures -J oint resear ch report for GPA an d Gas Research In-

stitu te. J ane H uey Hong and Riki Kobayashi, RiceUniver sity, Houst on, Texas. P roject 757.

RR-47 Behavior of CH4-CO2-H2S Mixtures at Sub-Ambi-ent Temperatures - Joint research report for GPAan d Can adian Gas Pr ocessors Association. D. B. Ro-binson, H-J . Ng an d A. D. Leu, Univers ity of Al-berta , Ed monton, Alberta . P roject 738-A.

RR-48 Vapor-Liquid and Liquid-Liquid Equilibria:Water-Methane; Water-Carbon Dioxide; Water-Hy-drogen Sulfide; Water-nPentane; Water-Methane-

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nPentane - Pa ul Gillespie and Gra nt Wilson, WiltecResearch Company, Provo, Utah. Project 758-B.

RR-49 Liquid-Liquid-Vapor Equilibria in Cryogenic LNGMixtures - James P. Kohn, University of NotreDame, Notre Dame, Indiana and Kraemer Luks,University of Tulsa, Tulsa, Oklahoma. Project 795.

RR-49A Liquid-Liquid-Vapor Equilibria in Cryogenic LNGMixtures(raw data). J am es P. Kohn, Universit y of

Notre Dame, Notre Dame, Indiana and KraemerD. Luks, University of Tulsa, Tulsa, Oklahoma.Pr oject 795.

RR-50 Measurement and Interpretation of the Water Con-tent of a Methane-Propane (5.31 mol %) Mixture inthe Gaseous State in Equilibrium with Hydrate -Hyoo Y. Song a nd Riki Kobayash i, Rice Univers ity,Houst on, Texas. P roject 775.

RR-5l The Equilibrium Phase Properties of Selected Naphthenic Binary Systems: Methylcyclohexane- Nitrogen, Ethylcyclohexane-Hydrogen Sulfide andn-Propylcyclohexane-Hydrogen Sulfide - D. B. Ro-binson, S-S Hu an g and A. D. Leu, Univers ity of Al-berta , Edmonton, Alberta. Pr oject 755-B.

RR-52 Vapor-Liquid Equilibria for Sour Water Systemswith Inert Gases Present - J onath an L. Owens, JohnR. Cunningha m a nd Gr ant Wilson, Wiltec ResearchCo., Pr ovo, Uta h. Pr oject 805.

RR-53 Experimental Densities and Enthalpies for Water-Natural Gas Systems - John J . Scheloske, KennethR. Hall, Philip T. Eubank and James C. Holste,Texas A & M Un iversity, College St at ion, Texas. Pr o-

ject 772.

RR-53A Thermophysical Properties Tables for Wet, Sweetand Sour Natural Gases: Data Supplement to RR-53 - J ohn J . Scheloske, Kenneth R. Hall, Philip T.Eu bank a nd J am es C. Holste, Texas A & M Univer-

sity, College Sta tion, Texas. Pr oject 772.RR-54 The Equilibrium Phase Behavior of Several Solute

Gases in the Solvent Phenanthrene - Robert L. Ro-binson, J r., Philip J . Car lberg, John J . Heidma n an dYick-Kwan Chen , Oklah oma St at e Universit y, Still-water, Oklahoma. Project 757-A.

RR-55 Phase Equilibrium Studies for Methane/SynthesisGas Separation: The Hydrogen-Carbon Monoxide-

Methane System - Joint r esearch report for GPA andGas Research Inst itute. J ane Hu ey Hong and Riki Ko-bayashi, Rice University, Houst on, Texas. Project 757.

RR-56 Measurement of Total Fraction Condensed and Phase Boundary for a Simulated Natural Gas -J oint resear ch report for GPA an d Gas Research In-

stitu te. John L. Oscarson and Bert Sa xey, BrighamYoung Un iversit y, Pr ovo, Uta h. P roject 737.

RR-57 The Phase Behavior of Two Mixtures of Methane,Carbon Dioxide, Hydrogen Sulfide and Water - D. B.Robinson, S-S Hua ng, A. D. Leu and H-J Ng, Univer-sity of Albert a, Edmonton, Alberta . Project 758-A.

RR-58 The Equilibrium Phase Properties of Selected Naphthenic Binary Systems: Ethylcyclohexane-Carbon Dioxide, Ethylcyclohexane-Nitrogen and

Ethylcyclohexane-Methane - D. B. Robinson, C-J

Chen a nd H -J Ng, University of Alberta , EdmontoAlbert a. P roject 755-B.

RR-59 Vapor-Liquid Equilibrium Measurements on the Sytems N2-Toluene, N2-m-Xylene, and N2-Mesitylene -Laugier, D. Legret, J. Desteve, D. Richon and Renon, A.R.M.I.N.E.S., Pa ris, F rance. Pr oject 755-

RR-60 Liquid-Liquid-Vapor Equilibria in Cryogenic LN Mixtures: Phase II- Ja mes P. Kohn and Robert

Merrill, University of Notr e Dame, Notre Dam e, Idiana and Kraemer D. Luks, University of TulsTulsa, Oklahoma. Project 795.

RR-6l An Evaluation of the GPSA Engineering Data BoVolume Correction Factor Table for Light EndsDavid B. Manley, University of Missouri, RollMissouri. Pr oject 819.

RR-62 Water-Hydrocarbon Liquid-Liquid-Vapor Equilirium Measurements to 277C - J oint r esearch repofor GPA and American P etr oleum I nst itute. C. Jefrey Brady, John R. Cunn ingham and Gr ant WilsoWiltec Resear ch Co., Provo, Uta h.

RR-63 Experimental Enthalpies for Pure Toluene and Pu

Methylcyclohexane - Luis E. Cediel, Philip Eubank, James C. Holste and Kenneth R. HaTexas A & M Un iversity, College Stat ion, Texas. Pr

ject 792-82.

RR-64 Development of GPA Data Bank of Selected Ethalpy and Equilibria Values - Thomas E. DaubePennsylvania State University, University ParPennsylvania. Project 806/822.

RR-64C GPA Data Bank of Selected Enthalpy and Equibria Values- Thomas E. Daubert, PennsylvanState University, University Park, PennsylvaniPr ojects 806 & 822.

RR-65 Vapor-Liquid Equilibria for Sour Water Systems High Temperatures - Jonatha n L. Owens, John

Cunningham and Grant M. Wilson, Wiltec Rsea rch Co., Pr ovo, Uta h. Pr oject 805-82.

RR-66 Equilibrium Phase Composition and HydratConditions in Systems Containing Methanol, Lig

Hydrocarbons, Carbon Dioxide and Hydrogen Sufide - Joint resear ch report for GPA an d Cana diGas Processors Association. H-J. Ng and D. B. Rbinson, D. B. Robinson & Assoc., Ltd., a nd U nivesity of Albert a, Ed mont on, Albert a. Pr oject 825-8

RR-67 Liquid-Liquid-Vapor Equilibria in Cryogenic LNMixtures: Phase III-Nitrogen Rich Systems- JamP. Kohn and Robert C. Merrill, Jr., University Notre Dam e, Notre Dame, Indiana and Kra emer Luk s, Universit y of Tulsa , Tulsa , Oklahoma . Proje

795-82.

RR-68 Excess Enthalpy Experimental Data-Binary SystemWater + n-Pentane, Water + n-Hexane, Water + n-Hetane, Water + n-Octane - C. J . Wormald, C. N. CollinN. M. Lancaster and A. J. Sellers, University of Brtol, Bristol, En gland. P roject 773-A-79.

RR-69 Evaluation of GPA*SIM Computer Program with GPData Bank of Selected Enthalpy Values - Thomas Daubert, Pennsylvania State University, UniversiPa rk, P ennsylvania. Pr oject 822-82.

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RR-70 Phase Equilibrium Studies for Processing of GasFrom CO2 EOR Projects - Project su pported jointly bythe Gas P rocessors Association and special indust rycontr ibutions. J ane Huey Hong and Riki Kobayashi,Rice University, Houston, Texas. Project 826-82.

RR-71 Water Content of NGL in Presence of Hydrates - KevinA. Sparks and E. Dendy Sloan, Colorado School ofMines, Golden, Colorado. Project 775-B-82.

RR-72 Measurement of Ethane and Propane Recovery andTotal Fraction Condensed for a Simulated NaturalGas in the Retrograde Region - John L. Oscarson,Brigham Young Un iversity, Pr ovo, Uta h. P roject8l5-81.

RR-73 Heats of Mixing of Steam with N2, CO2, H2 , CH4,and CO at High Temperatures and Pressures Usinga New High Temperature Calorimeter - Grant M.Wilson and C. Jeff Brady, Wiltec Research Co.,Pr ovo, Utah . Pr oject 773-79 & 80.

RR-74 The Influence of Methanol on Hydrate Formation atLow Temperatures - H-J. Ng and D. B. Robinson, D.B. Robinson & Assoc., Ltd., E dmonton, Albert a. P ro-

ject 825-83.

RR-75 Vapor-Liquid Equilibria Measurements on the Sys-tems N2-n-Propylcyclohexane, CO2-n-Propylcyclo-hexane, CH4-n-Propylcyclohexane, CH4-n-Propyl-benzene and CO2-n-Propylbenzene - S. Laugier, P.Alali, A. Valtz, A. Chareton, F. Fontalba, D. Richonand H. Renon, A.R.M.I.N.E.S., Par is, Fr ance. Pro-

ject 755-C-82.

RR-76 Phase Equilibrium Studies for Processing of Gasfrom CO2 EOR Projects-Phase II- Pr oject su pportedjointly by the Gas Processors Association and spe-cial industry contributions. Jane Huey Hong andRiki Kobayashi, Rice University, Houston, Texas.Pr oject 826-83.

RR-77 Evaluation of GPA*SIM Computer Program withGPA Data Bank of Selected V-L-E Data - Thoma s E.Daubert, Pennsylvania State University, Univer-sity Pa rk, P ennsylvania. Pr oject 806-83.

RR-78 Sulfur Compounds and Water V-L-E and MutualSolubility MESH-H2O; ETSH-H2O; CS2-H2O; andCOS-H2O - Pau l C. Gillespie and Gr ant M. Wilson,Wiltec Resear ch Co., Pr ovo, Uta h. P roject 758-80.

RR-79 Liquid-Liquid-Vapor Equilibria in Cryogenic LNG Mixtures (Phase IV - Nitrogen-Rich Systems) -J am es P. Kohn an d F eliciano M. Llave, Universityof Notre Dame, Notre Dame, Indiana and Kra emerD. Luks, Univers ity of Tulsa , Tulsa , Oklahoma . Pr o-

ject 795-83.

RR-80 The Water Content of CO2-Rich Fluids in Equilib-rium with Liquid Water or Hydrate - Kyoo Y. Songand Riki Kobayashi, Rice University, Houston,Texas. P roject 775-83.

RR-81 Evaluation of Peng-Robinson Computer Programwith GPA Data Bank of Selected Enthalpy Values -Thomas E. Daubert, Pennsylvania State University,University Park, Pennsylvania. Project 822-83.

RR-82 Vapor-Liquid Equilibria Measurements on the Sys-tems Ethane-Toluene, Ethane-n-Propylbenzene,

Ethane-Metaxylene, Ethane-Mesitylene, Ethane-Methylcyclohexane - S. La ugier, A. Valt z, A. Char e-ton, D. Richon a nd H . Renon, A.R.M.I.N.E.S., Pa ris ,France. Project 755-C-83.

RR-83 Excess Enthalpy Experimental Data Binary Systems:Water-Carbon Monoxide, Water-Carbon Dioxide - C. J .Worma ld, N. M. Lan caster, A. J . Sellars, Un iversity ofBristol, Brist ol, England. P roject 773-A-81.

RR-84 Evaluation of Equi-Phase (Peng-Robinson) ComputerProgram with GPA Data Bank of Selected V-L-E Data- Thoma s E. Daubert , Pennsylvania Sta te University,University Park, Pennsylvania. Project 806-84.

RR-85 Enthalpies of Solutions of CO2 in Aqueous Diglyco-lamine Solutions - Scott P. Christensen, James J.Christ ensen a nd Reed M. Izatt , Brigham YoungUniver sity, Pr ovo, Uta h. Pr oject 821-84.

RR-86 Properties of CO2-Rich Mixtures - Joint researchreport for GPA and Gas Research Institute. K. R.Ha ll, J . C. Holste, P. T. Euba nk a nd K. N. Marsh ,Texas A & M University, College Station, Texas.Project 842-84.

RR-87 Hydrate Formation and Equilibrium Phase Compo- sitions in the Presence of Methanol: Selected Sys-tems Containing Hydrogen Sulfide, Carbon

Dioxide, Ethane or Methane - H-J. Ng, C-J. Chenan d D. B. Robinson, D. B. Robinson & Assoc., Ltd.,Edm onton, Alberta . P roject 825-84.

RR-88 Vapor-Liquid Equilibria Measurements on the Sys-tems Ethane-n-Propylcyclohexane, Propane-Cyclo-hexane, Propane-n-Propylcyclohexane, Propane-n-

Propylbenzene and Propane-Mesitylene - S. Laugier,A. Valtz, A. Chareton, D. Richon and H. Renon,A.R.M.I.N.E.S., Par is, Fr an ce. Pr oject 755-C-84.

RR-89 Vapor-Liquid Equilibrium and Condensing Curvesfor a Typical Gas Condensate - H-J Ng a nd D. B.

Robinson, D. B. Robinson & Assoc., Ltd., E dmont on,Albert a. P roject 815-82 & 83.

RR-90 Vapor-Liquid Equilibrium Measurements on theAmmonia-Water System from 313K to 589K- Jointresearch report for GPA and AIChE-DIPPR. C.Gillespie, W. Vincent Wilding an d Gr an t M. Wilson,Wiltec Resear ch Co., Pr ovo, Ut ah . Pr oject 758-B-81.

RR-91 Liquid-Liquid-Vapor Equilibria in Cryogenic LNGMixtures - Phase V-Ja mes P. Kohn an d F. M. Llave,University of Notre Dame, Notre Dame, Indianaan d Kraem er D. Luks, University of Tulsa, Tulsa,Oklahoma. Project 795-85.

RR-92 The Effect of Ethylene Glycol or Methanol on Hy-

drate Formation in Systems Containing Ethane, Propane, Carbon Dioxide, Hydrogen Sulfide or aTypical Gas Condensate - H-J Ng, C. J . Chen and D.B. Robinson, D. B. Robinson & Assoc., Ltd., E dmon-ton, Alberta . Pr oject 825-85.

RR-93 Gas Solubilities and Vapor-Liquid EquilibriumMeasurements of H2, CO2 and NH3 in Water-PhenolMixtures from 110 degrees F to 550 degrees F- PaulC. Gillespie, Jonat han L. Owens a nd Gra nt M. Wil-son, Wiltec Resear ch Co., Pr ovo, Utah . Pr oject 758-B-81 & 82.

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RR-94 Phase Equilibrium Studies for Processing of Gasfrom CO2 EOR Projects (Phase III): A. The Effect ofToluene as an Extractive Agent; B. The Effect of

Methane on

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