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&[DATE] &[TIME] - &[FILENAME]

ProdeProperties Test File

for Prode Properties ver. 1.2b

This file may be used to insure that the Mathcad prode.dll file is in the right directory and that the functions are working properly.Prode Properties may be tested independent of Mathcad using the Excel version in the Prode directory.Examples are provided to demonstrate how the functions may be used.The process examples (compressor, nozzles, etc.) were based on the Excel examples included in the Prode Properties installation.

Directions for using this worksheet

The default archive from Prode, def.ppp, will be used as the starting file.This worksheet will write changes to a new archive, test.ppp.This file will be placed in the same directory as def.ppp, but the user may also later archive to other directories. Operations that set a variable will show a result of 1 if successful or 0 if not.Results that retrieve values will show the retrieved value, or 0 if no value is available. The exceptions to this convention will be noted. Automatic calculation has been turned off so the new user may read these instructions before starting the computations. Procedure: Calculate the entire worksheet, ctrl-F9 Select dep.ppp archive when first window appears, and click Open When second popup window, the Prode archive, appears, it should show stream 2.Click OK. Scroll through the worksheet to check for errors.See "Errors" below. If the Prode window pops up, it is allowing you to view a recently created stream.Click OK to close. Errors: Mathcad will show errors in red as usual.Typical errors might be caused by syntax in the argument list, or the function may not be found in the library delivered by Prode, ppp.lib. If the result is zero, then the Prode function had an error or could not return a value.Frequently, this may be caused by the lack of a particular phase needed for an operation.For example, solid properties can't be returned when a stream has no solid phase, or when the temperature is above the melting point for a pure compound property. Rarely, a ppp.dll error window may appear with "Error accessing component's data archive".This appears to be caused by a lack of data in the chem.dat file for that particular property.If this window appears, it must be closed to proceed with the computations.See also the mc_defErrMsg function for a way to prevent these windows from stopping the calculations.The program is set to prevent these error windows.

File open commands

disabled

C:\ProgramData\prode\def.ppp mc_AFOpen 1

This command sets the path to the archive file and directory.The path shown is the default set during the Prode Properties installation.This command will affect all subsequent uses of Prode on this computer until the path is changed again by another AFOpen command.Therefore, this command should be used with caution.

dummy mc_AOpen 1

browse for an archive in the default directory

Note: Some of the Prode statements have been disabled to eliminate the repeated appearance of the Prode window during recalculation.

The next two functions do not obey the normal Prode convention regarding the result returned if successful. A result of 0 means

these were successful. They must be evaluated (followed by "=") in order for the operation to take place.

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0 mc_setErrFlag 0

set to 0at start of calc's to clear flag

wopt 0 :

wopt mc_defErrMsg 0

wopt = 0 turns off the Window Dialog messages wopt = 1 turns on the Window Dialog messages

Open Properties window to view edit streams

stream 2 :

stream mc_edS 0

edit the given stream in the current active archive using the Prode window

dummy mc_edSS 0

open to the first stream (disabled for the test to reduce popups)

Chemical file operations

dummy mc_getFCNr 1635

number of components in data file, should be 1635 or greater.If less, then you are using the free version of Prode and not all of the routines below will work.

id 7732185 :

CAS number of water (use internet search to find values for compounds)

compcode is an integer from 1 to number of components in the data file

compcode id mc_CompCID : 1631

given id=CAS#, return compcode from database

Note: The above statement shows that the functions may be used to define a variable in addition to merely showing a result.

compcode mc_CompF H2O

givena component code, returns component formula string

compcode mc_CompN WATER

component name

compcode mc_CompID 7.7322 106^*

CAS number of component, compare to id above

Note: The units are not returned by the Prode commands.Operations that show which units are being used are shown later.

compcode mc_CompMw 18.0153

molecular weight

T.c compcode mc_CompTc K * : 647.096 K *

critical temperature

T.c R 64709.6008 K s * T * *

multiply the function by the current Prode units for the result to use the unit features of Mathcad

compcode mc_CompPc 2.2064 107^*

critical pressure

compcode mc_CompVc 0.0031

critical volume

compcode mc_CompAc 0.344

acentric factor

compcode mc_CompDm 6.1782 1030 -^*

dipole moment

compcode mc_CompRg 6.15 1011 -^*

radius of gyration

compcode mc_CompSol 1511.8849

solubility parameter

compcode mc_CompHf 13422.8364 -

heat of formation

compcode mc_CompGf 12698.6729 -

Gibbs energy of formation

compcode mc_CompSf 333.4738

enthalpy of fusion

compcode mc_CompNb 373.15

normal boiling point

compcode mc_CompMp 273.15

melting point temperature

The following provide non zero values only if the phase of interest is present at the temperature requested.

tgl 300 :

temperature for gas/liquids (above freezing for water)

ts 260 :

temperature for solids (below freezing)

compcode tgl mc_CompVP 3548.3262

saturation pressure at temp tgl

compcode tgl mc_CompHV 2436.313

heat of vaporization at tgl

compcode tgl mc_CompLV 0.0009

liquid viscosity at tgl

compcode tgl mc_CompGV 9.9253 106 -^*

gas viscosity at tgl

compcode tgl mc_CompLD 995.4764

liquid density at tgl

compcode ts mc_CompSD 918.6313

solid density at ts

compcode tgl mc_CompLC 0.6162

liquid thermal conductivity at tgl

compcode tgl mc_CompGC 0.0188

gas thermal conductivity at tgl

compcode ts mc_CompSC 0

solid thermal conductivity at ts (appears to be missing for water)

compcode tgl mc_CompST 0.0718

surface tension at tgl

integrated changes between two temperatures, t0 and t1 for pure components

t0 280 :

t1 290 :

compcode t0 t1 mc_CompHG 18.6114

ideal gas enthalpy change

compcode t0 t1 mc_CompSG 0.0653

ideal gas entropy change

compcode t0 t1 mc_CompHL 42.0177

ideal liquid enthalpy change

compcode t0 t1 mc_CompSL 0.1474

ideal liquid entropy change

ts0 260 :

ts1 270 :

lower the temperature range < freezing pt

compcode ts0 ts1 mc_CompHS 20.5241

ideal solid enthalpy change

compcode ts0 ts1 mc_CompSS 0.0774

ideal solid entropy change

Units commands

See "Units of Measurement" section in Prode manual for a list of the units and their numerical codes.

UM 15 :

pressure is used for an example

n_press UM mc_getUMN : 22

no. of units avail. for UM

UM mc_getUMC 1

present units code for UM

UM mc_getSUMS Pa.a

present units string for UM

sel 5 :

select unit 5

UM sel mc_getUMS KPa.a

units string for (UM, sel)

list all of the units for pressure

i_1 n_press range :

P_units i_el UM i_mc_getUMS :

P_units Pa.a Pa.g mbar.a mbar.g KPa.a KPa.g bar.a bar.g MPa.a MPa.g kgf/cmq.a kgf/cmq.g psi.a psi.g atm.a atm.g mmH2O.a mmH2O.g inH2O.a inH2O.g mmHG.a mmHG.g 221 mat

stream mc_getP Pa * psi 290.0755

multiply by current Prode pressure unit, then request any unit in the result

sel 13 :

select a new pressure unit

UM sel mc_setUMC 1

change to the 11th unit for pressure

UM mc_getSUMS psi.a

show current unit name for UM

stream mc_getP psi * psi 290.0804

now pressure results must be multiplied by psi

UM 1 mc_setUMC 1

reset to original unit for remainder of worksheet

Routines UMCR, UMCS, and UMAU are not fully documented in the Prode manual so they have been left out of the dll.

UM mc_UMRAU 1

removes all added units for (property no.)

Error message flags

last error message, maybe from a previous run

mc_ErrMsg Error accessing component's data archive

dum dummy :

errflag dum mc_getErrFlag :

0 = no errors, 1 = errors found

errflag 1

This flag only works if the Window Dialog messages are turned off.Otherwise, the Dialog messages are themselves the indication of errors.See mc_defErrMsg.Errors that Mathcad detects (i.e. red indication) are not included for this flag. At the time this test file was created, the thermal conductivity of solid water was not available in the database, causing an error and a value of 1 for errflag.

0 mc_setErrFlag 0

set to 0at start of next calc's to clear flag

0 mc_defErrMsg #

0 = turns off the Window Dialog messages 1 = turns on the Window Dialog messages This function was demonstrated at start of worksheet.Turning off the Window Dialog messages allows the computations to continue without pausing to close the Dialog window when an error occurs.The error may still be visible if a 0 value is returned where a real number is expected.

Atmospheric pressure

patm mc mc_getPatm : 1.0133 105^*

the pressure shouldbe 1.013105

Base values for enthalpy and entropy

The default values for the base temperature, enthalpy, and entropy may be found in the config>settings Prode window. The functions below may be used to change the settings. The settings apply only to the current archive. The settings for the archive are saved when the archive is saved.

Code Procedure 1 = initial values specified by user (values of tref and val) 2 = initial values are enthalpy of formation (or entropy of formation) and temperature 25 C

If code = 2, the tref and val inputs are ignored.

code 1 :

tref 298 :

val 0 :

code tref val mc_setHB 1

enthalpy references

code tref val mc_setSB 1

entropy references

Read/write stream properties

If a write operation exists, it will appear under the read operation, using the value from the read operation.This simplifies the testing process.

The write operations in this section are in blue highlight.

stream 1 :

phase 2 :

the phase position (not the phase type)

cpos 2 :

cpos is the component's numerical position in the composition vector for the stream, starting with 1

stream mc_isSDef 1

given a stream returns TRUE (integer = 1) if stream has been defined, otherwise returns FALSE (0)

name stream mc_StrN : Test Case 1

stream name

stream name mc_putN 1

stream 150 patm mc_setOp 1

This is an edit operation to lower the temperature so liquid will be present for the functions below.

t stream mc_getT : 150

temperature

stream t mc_putT 1

p stream mc_getP : 1.0133 105^*

pressure

stream p mc_putP 1

pnr mc mc_getPNr : 10

returns the maximum number of phases that procedure can detect in the archive for all streams (may include phases at other temperatures)

stream phase mc_StrPt 2

given a stream and phase # in range 1- getPNr() returns the phase type (0=vapor,1=liquid,2=solid)

i_1 pnr range :

stream 1

given a stream and phase # in range 1- getPNr() returns a ANSI C string with the description of type for detected phase

phases i_el stream i_mc_StrPts :

phases Vapor Solid Solid Not present Not present Not present Not present Not present Not present Not present 101 mat

only one liquid phase is present later, the flash routine code will be reset to obtain two liquid phases

stream mc_StrLf 0

given a stream returns the total liquid fraction (molar basis) in stream

stream phase mc_StrPf 0.1456

given a stream and phase phase # in range 1- getPNr() returns the phase fraction

w stream phase cpos mc_getW : 1.0251 106 -^*

mole fraction of component (cpos #) in a phase

stream phase cpos w mc_putW 1

mole fraction w of component cpos in a phase

rate stream mc_getWm : 1

stream flow rate, mass/time

stream rate mc_setWm 1

zi stream cpos mc_getZ : 0.15

mole fraction of component cpos in total stream

stream cpos zi mc_putZ 1

stream mc_getCNr 3

number of components in stream

stream mc_StrZv 0.9841

returns the relevant compressibility factor (gas phase)

stream mc_StrMw 22.9437

molecular weight of total stream

stream mc_StrGMw 16.4078

molecular weight of gas phase

stream mc_StrLMw 0

molecular weight of liquid phase

stream mc_StrV 0

specific volume as sum of specific volumes of all phases

enthalpy

h stream mc_StrH : 526.8941 -

total stream enthalpy

stream mc_StrGH 157.4136 -

gas phase enthalpy

stream mc_StrSGH 309.6676 -

gas specific enthalpy

stream mc_StrLH 0

liquid enthalpy

stream mc_StrSLH 0

liquid specific enthalpy

stream mc_StrSH 369.4805 -

solid enthalpy

stream mc_StrSSH 751.482 -

solid specific enthalpy

entropy

entropy stream mc_StrS : 2.5474 -

total stream entropy

stream mc_StrGS 0.7266 -

gas phase entropy

stream mc_StrSGS 1.4294 -

gas specific entropy

stream mc_StrLS 0

liquid entropy

stream mc_StrSLS 0

liquid specific entropy

stream mc_StrSS 1.8208 -

solid entropy

stream mc_StrSSS 3.7034 -

solid specific entropy

heat capacity, mass basis

stream mc_StrGICp 2.0277

ideal gas heat capacity

stream mc_StrGCp 2.0551

gas constant pressure heat capacity

stream mc_StrGCv 1.523

gas constant volume heat capacity

stream mc_StrLCp 0

liquid constant pressure heat capacity

stream mc_StrLCv 0

liquid constant volume heat capacity

stream mc_StrSCp 1.36

solid constant pressure heat capacity

speed of sound

stream mc_StrMSS #

mixed phase speed of sound HEM model

stream mc_StrGSS 266.4921

gas phase

stream mc_StrLSS 0

liquid phase

Joule Thomson coefficient

stream mc_StrGJT 1.4851 105 -^*

gas phase

stream mc_StrLJT 0

liquid phase

compressibility, expansivity

stream mc_StrGIC 1.003 105 -^*

gas isothermal compressibility, 1VPV

stream mc_StrLIC 0

liquid isothermal compressibility

stream mc_StrGVE 0.0069

gas volumetric expansivity 1VTV

stream mc_StrLVE 0

gas volumetric expansivity

density

stream mc_StrGD 1.3546

gas density

stream mc_StrLD 0

liquid density

thermal conductivity

stream mc_StrGC 0.0159

gas conductivity

stream mc_StrLC 0

liquid conductivity

viscosity

stream mc_StrGV 6.0897 106 -^*

gas viscosity

stream mc_StrLV 0

liquid viscosity

surface tension

stream mc_StrST 0

liquid/gas

flammability

stream mc_StrFML 4.995

gas phase lean limit

stream mc_StrFMH 15.0622

gas phase rich limit

other stream properties

stream mc_StrHC 48365.4562

gas phase heat of combustion

compcode stream cpos mc_getCC : 594

component number for component = cpos

stream cpos compcode mc_putCC 1

dummy mc_getMCNr 50

maximum number of components in a stream

interactions

int_pos 1 :

the interaction number (i.e. the row in the BIP window for the stream)

dummy mc_getMBPNr 250

maximum number of binary pairs in a stream (for all streams)

ci stream int_pos mc_getCi : 1

component index i in interaction list

stream int_pos ci mc_putCi 1

cj stream int_pos mc_getCj : 2

component index j in interaction list

stream int_pos cj mc_putCj 1

model stream int_pos mc_getMB : 50

returns model number for interaction # int_pos in given stream

stream int_pos model mc_putMB 1

sets the model number for a given stream and interaction number, int_pos

id 0 :

This id is the BIP column (starting with 0 for BIP-1) shown in the PPP window under BIPs for the stream.

Kji stream int_pos id mc_getBIP : 0.1183

value of the interaction coefficient

stream int_pos id Kji mc_putBIP 1

specifies a value for an interaction coefficient

thermodynamic models for streams

stream 1

Kcode 50 :

code for SRK standard model package, see manual for other package numbers

stream Kcode mc_setKM 1

mp codes for functions below

1fugacity 2enthalpy 3entropy 4molar volume 5viscosity

Examples for fugacity and enthalpy models below:

state 0 :

vapor state

mp 1 :

fugacity model for stream, state

fmodel stream mp state mc_getMP : 50

retrieve model number

stream mp fmodel state mc_setMP 1

set model number

mp 2 :

enthalpy model for stream, state

hmodel stream mp state mc_getMP : 50

retrieve model number

stream mp hmodel state mc_setMP 1

set model number

Thermodynamic calculations

stream 5 :

use stream 5 for examples below

p 1.0133 105^*

t 150

state 1 :

state (0=vapor, 1=liquid, 2=solid)

phase equilibria

n 1 :

pf .3 :

see below

stream p pf state n mc_PfPF 290.766

n th equilibrium temp at p, pf (phase fraction), state (0=vapor, 1=liquid, 2=solid)

stream t pf state n mc_PfTF 0

n th equil. press at t, pf, state

lf .2 :

set liquid fraction

stream p lf mc_LfPF 299.6111

first equil. temp at liquid fraction, lf

stream t lf mc_LfTF 0

first equil. pressure at liquid fraction, lf

stream mc_StrCPnr 1

number of critical points found

cpn 1 :

selected critical point

stream cpn mc_StrPc 4.6926 106^*

critical pressure for critical point #, cpn

stream mc_StrCBp 4.6934 106^*

cricondenBar pressure

stream mc_StrCBt 444.1406

cricondenBar temperature

stream mc_StrCTp 4.4361 106^*

cricondenTherm pressure

stream mc_StrCTt 446.9182

cricondenTherm temperature

stream mc_StrAc 0.2077

acentric factor (mole fraction average)

phase diagrams

stream 5 :

lnr stream mc_PELNr :

Given a stream calculates the phase diagram and returns the number of equilibrium lines available

lnr 2

line types

line 2 :

ltype stream line mc_PELT :

Given a stream and line number, returns the line type: bubble line dew line three phase line fractional phase

ltype 2

line properties

lprop stream line mc_PELP :

Given a stream and line, returns the line properties: vapor-liquid vapor-liquid-liquid vapor-solid liquid-solid fractional phase

lprop 1

equilibrium lines

The prode.dll has assumed a maximum number of points of 50 for the equilibrium lines.This dimension cannot be changed dynamically for the variables passed to and from Mathcad.Therefore, the mc_PELine routine leaves out the maxpt variable that is shown in the Prode corresponding routine.

The mc_PELine function (see the first line in the program below) produces a matrix result.Although this matrix can be used "as is" the Mathcad program, "PELine" below calls mc_PELine and splits the matrix into the separate variables.

stream 5

streamx linex PELine M streamx linex mc_PELine : npts M 13 el : Te M 1 npts 11 submatrix K * : Pr M 1 npts 22 submatrix Pa * : Te Pr npts 13 mat 51 line :

Given stream and equilibrium line number, the temperature and pressure vectors and the total number of points are computed and returned.

The output is shown below.

T1 P1 npts1 13 mat stream line PELine :

T1 311.1738 K * 316.4703 K * 322.564 K * 327.6265 K * 332.689 K * 337.7515 K * 342.814 K * 347.8765 K * 356.6734 K * 361.6734 K * 366.6734 K * 371.6734 K * 376.6734 K * 381.6734 K * 386.6734 K * 151 mat

P1 1.0133 105^* kg m s 2^* / * 1.2358 105^* kg m s 2^* / * 1.5389 105^* kg m s 2^* / * 1.8338 105^* kg m s 2^* / * 2.1723 105^* kg m s 2^* / * 2.559 105^* kg m s 2^* / * 61 mat

npts1 31

phase fraction lines

stream 5 :

state 0 :

fraction .5 :

stream state fraction PFLine M stream state fraction mc_PFLine : npts M 13 el : Tem M 1 npts 11 submatrix K * : Pr M 1 npts 22 submatrix Pa * : Tem Pr npts 13 mat 51 line :

Given stream, state, and fraction of that state, computes the temperature and pressure vectors along that phase ction, plus the number of points on the curve.

Tf Pf nf 13 mat stream state fraction PFLine :

nf 35

Tf 270.8829 K * 275.8829 K * 280.8829 K * 285.8829 K * 290.8829 K * 295.8829 K * 300.8829 K * 305.8829 K * 310.8829 K * 315.8829 K * 320.8829 K * 325.8829 K * 330.8829 K * 131 mat

Pf 1.0133 105^* kg m s 2^* / * 1.2093 105^* kg m s 2^* / * 1.4338 105^* kg m s 2^* / * 1.6895 105^* kg m s 2^* / * 1.9791 105^* kg m s 2^* / * 51 mat

linef Tf Pf augment :

lnr stream mc_PELNr : 2

The lnr statement and the code on the left replaces the PhaseEnv program in the Mathcad version of this file.

line 1 lnr range Tl line el Pl line el nl line el 13 mat stream line PELine : typel line el stream line mc_PELT : propl line el stream line mc_PELP : linexy line el Tl line el Pl line el augment : 41 sys for

Tl 1 el 232.9657 K * 238.599 K * 244.6927 K * 252.2865 K * 259.8802 K * 267.474 K * 272.474 K * 277.474 K * 282.474 K * 91 mat

Pl 1 el 1.0133 105^* kg m s 2^* / * 1.2342 105^* kg m s 2^* / * 1.5124 105^* kg m s 2^* / * 1.9221 105^* kg m s 2^* / * 41 mat

Tl 2 el 311.1738 K * 316.4703 K * 322.564 K * 327.6265 K * 332.689 K * 337.7515 K * 342.814 K * 347.8765 K * 356.6734 K * 361.6734 K * 101 mat

Pl 2 el 1.0133 105^* kg m s 2^* / * 1.2358 105^* kg m s 2^* / * 1.5389 105^* kg m s 2^* / * 1.8338 105^* kg m s 2^* / * 41 mat

As shown in the nc vector, the lines may have different number of points.In order to prevent curves returning to the origin, extract the data from Tj and Pj.

linexy 1 el linexy 2 el linef 3 1 sys

The PELine and PFLine programs and the code for the phase envelope curves may be copied into or referenced by other programs.

hydrates

hydmodel 1 :

thyd 260 :

str_hyd 2 :

stream for hydrate function below

hydmodel = 1 = assume free water present, this option produces conservative but safe values 2 = calculate amount of water in liquid phase 3 = solve as multiphase equilibria, solve phase equilibria including solids as ice

Since water is not present in the stream chosen for testing, the 2 and 3 hydmodels will return 0.

phyd str_hyd thyd hydmodel mc_HPFORM : 0

returns the pressure that hydrates form at temperature = thyd

The HTFORM Prode function is not available in the Basic version, but the HPFORM function should suffice.

flashes

stream 5

stream mc_setSOp 1

flash at standard conditions

et 0 :

estimated temperature set to 0 for automatic

ep 0 :

estimated pressure set to 0 for automatic

stream 150 patm mc_setOp 1

set new operating conditions and flash

t stream mc_getT : 150

temperature

p stream mc_getP : 1.0133 105^*

pressure

h stream mc_StrH : 811.9593 -

enthalpy obtained above

entropy stream mc_StrS : 3.281 -

entropy obtained above

sv stream mc_StrV : 0.0014

volume obtained above

find temperature

stream p sv et mc_VPF 150

volume-pressure flash, et=temp guess

stream p h et mc_HPF 150

enthalpy-pressure flash, et=temp guess

stream p entropy et mc_SPF 150

entropy-pressure flash, et=temp guess

find pressure

stream t sv ep mc_VTF 0

volume-temp flash, ep=press guess

stream t h ep mc_HTF 0

enthalpy-temp flash, ep=press guess

stream t entropy ep mc_STF 0

entropy-temp flash, ep=press guess

The flashes that determine pressure have some difficulty converging for multiphase (liquids and solids) problems.Select another flash routine and iterate if needed.

Extended methods for accessing stream properties

These functions allow simultaneous setting of temperature and pressure followed by an isothermal flash before the desired property is returned.These methods should be used with care because of the change in the stream conditions.

stream 2 :

stream t p mc_EStrGMw 16.0474

gas molecular weight

stream t p mc_EStrLMw 55.7928

liquid molecular weight

stream t p mc_EStrLf 0.0009

mole fraction of liquid

phase 1 :

position of phase, not the state code. positions are usually vapor=1, liquid=2, solid=3 but extra liquid and solid phases may be present

stream phase t p mc_EStrPf 0.9991

molar phase fraction of phase

stream t p mc_EStrZv 0.9843

gas (vapor) compressibility factor

stream t p mc_EStrH 317.8313 -

total enthalpy

stream t p mc_EStrV 0.7525

total specific volume

stream t p mc_EStrGCp 2.103

gas constant pressure heat capacity

stream t p mc_EStrGCv 1.5593

gas constant volume heat capacity

stream t p mc_EStrLCp 1.7035

liquid constant pressure heat capacity

stream t p mc_EStrLCv 1.3968

liquid constant volume heat capacity

stream t p mc_EStrGIC 1.0028 105 -^*

gas isothermal compressibility

stream t p mc_EStrLIC 5.1467 1010 -^*

liquid isothermal compressibility

stream t p mc_EStrMSS 317.7297

mixture speed of sound

stream t p mc_EStrGSS 318.2669

gas speed of sound

stream t p mc_EStrLSS 3354.1111

liquid speed of sound

stream t p mc_EStrGJT 1.4662 105 -^*

gas Joule Thomson coefficient

stream t p mc_EStrLJT 6.9784 107 -^* -

liquid Joule Thomson coefficient

stream t p mc_EStrGVE 0.0069

gas volumetric expansivity coefficient

stream t p mc_EStrLVE 0.0009

liquidvolumetric expansivity coefficient

stream t p mc_EStrHC 50008.9081

heat of combustion

stream t p mc_EStrFML 4.999

lean flammability limit of gas

stream t p mc_EStrFMH 14.9987

rich flammability limit of gas

stream t p mc_EStrS 1.4661 -

total entropy

stream t p mc_EStrGD 1.3246

gas density

stream t p mc_EStrLD 730.588

liquid density

stream t p mc_EStrGC 0.0161

gas thermal conductivity

stream t p mc_EStrLC 0.1754

liquid thermal conductivity

stream t p mc_EStrGV 6.0282 106 -^*

gas viscosity

stream t p mc_EStrLV 0.0013

liquid viscosity

stream t p mc_EStrST 0.0288

surface tension

Fugacity and derivatives

The operations below behave like subroutines rather than functions because they return more than one result. The Mathcad system imposes some restrictions on function input and output so the normal C++ methods of passing variables is not possible.These restrictions are needed to enforce the "non code" look of the Mathcad interface .As a result of these restrictions, the functions below have slightly different argument lists than found in Prode and all of the results are returned in a single matrix .Mathcad routines are then provided to split these results into the appropriate variables.

The prode.dll has assumed a maximum number of components of 50 for all vector and matrix routines.This dimension cannot be changed dynamically for the variables passed to and from Mathcad .For greater number of components, prode.dll must be rebuilt. In that case, the constant "maxnc" in the source code for the routines in this section must be changed to the higher number.

stream 1 :

NC stream mc_getCNr :

t 150

These variables were defined above.

p 1.0133 105^*

stream t p mc_setOp 1

i_1 NC range :

phase 2 :

mf i_el stream phase i_mc_getW :

mf = mole fractions of components is stream

mf i_el 1.5711 107 -^* 1.0251 106 -^* 131 mat

state 1 :

The liquid state is being used.

process 1 :

Up to 5 processes may be defined in the base Prode version. Processes may be redefined with new streams.

process stream mc_DPinit 1

fugacity vector

fg process state t p mf NC mc_StrFv Pa * :

This routine returns the fugacity vector alone.

fg 2.2571 107^* kg m s 2^* / * 55244.7405 kg m s 2^* / * 1077.6956 kg m s 2^* / * 31 mat

fugacity i_el fg i_el mf i_el * :

The Prode routines define the "fugacity" variable as the fugacity coefficient times the total pressure. Thus, fugacity is obtained by the equation on the left.

fugacity 3.5463 kg m s 2^* / * 0.0566 kg m s 2^* / * 1077.6943 kg m s 2^* / * 31 mat

fugacity vector plus derivatives wrt T, P, w

process state t p mf NC StrFvd M process state t p mf NC mc_StrFvd : separate the results into vectors and a matrix fg M 1 NC 11 submatrix : dfgt M 1 NC 22 submatrix : dfgp M 1 NC 33 submatrix : dfgmf M 1 NC 44 NC + 1 - submatrix : fg dfgt dfgp dfgmf 14 mat 71 line :

1given the stream, state, temp, press, composition vector, w,and the number of components, NC, return fugacity vector, fg, and derivatives of fg wrt t, p, and mf.

fg dfgt dfgp dfgmf 14 mat process state t p mf NC StrFvd :

the default Prode units are applied to the results below but the variables are kept dimensionless for use in Prode Physical Properties program.

fg Pa * Pa 2.2571 107^* 55244.7405 1077.6956 31 mat

dfgt Pa K / * Pa K / 3.5879 105^* 4372.2585 115.1895 31 mat

dfgp 0.6059 0.0014 2.6093 105 -^* 31 mat

dfgmf Pa * Pa 3.7021 108^* - 2.841 108^* - 2.2457 108^* - 3.6321 105^* - 4.6135 105^* - 2.1749 105^* - 0.01 0.0114 0.006 33 mat

Other stream state variables and their derivatives

Functions were provided above (eg. mc_StrH)to obtain the enthalpy (H), entropy(S), and molar volume (V) of a stream. The next routine allows the operating conditions (t, p, w) to be specified to values other than those in the stream data file. The user selects which variable, H, S, or V, is desired, using a string variable with the corresponding variable initial. The program calls the appropriate mc_xxx function and then separates the variables from the output matrix.

X process state t p mf NC StrXvd X H ≡ M process state t p mf NC mc_StrHvd : do nothing if X S ≡ M process state t p mf NC mc_StrSvd : do nothing if X V ≡ M process state t p mf NC mc_StrVvd : do nothing if x M 1 col : dxt M 2 col : dxp M 3 col : dxmf M 1144 NC + 1 - submatrix : x dxt dxp dxmf 14 mat 81 line :

H dHt dHp dHmf 14 mat H process state t p mf NC StrXvd :

display results with default Prode units

H kJ kmol / * kJ kmol / 24964.9683 - 11 mat

dHt kJ kmol / K / * kJ kmol K * / 59.2059 11 mat

dHp kJ kmol / Pa / * kJ kmol Pa * / 2.4984 105 -^* 11 mat

dHmf kJ kmol / * kJ kmol / 8000.1235 - 19802.456 - 24959.9131 - 13 mat

S dSt dSp dSw 14 mat S process state t p mf NC StrXvd :

S kJ kmol K * / * kJ kmol K * / 118.5426 - 11 mat

dSt kJ kmol K 2^* / * kJ kmol K 2^* / 0.3947 11 mat

dSp kJ kmol K * Pa * / * kJ kmol K * Pa * / 3.4749 108 -^* - 11 mat

dSw kJ kmol K * / * kJ kmol K * / 71.4065 - 99.9233 - 101.9207 - 13 mat

V dVt dVp dVmf 14 mat V process state t p mf NC StrXvd :

V m 3^mol / * 0.0302 m 3^mol / * 11 mat

dVt m 3^mol K * / * 3.4749 105 -^* m 3^mol K * / * 11 mat

dVp m 3^mol Pa * / * m 3^mol Pa * / 1.0646 1011 -^* - 11 mat

dVmf m 3^mol / * m 3^mol / 0.0637 0.0614 0.0604 13 mat

Operations to set/retrieve the options needed for equation of state models and flash routine phases

See the Prode manual (see paragraph "Codes used in Prode library") and also open the Prode drop menus for the model to view the description of the options set by the OM code variable. The user will probably find it easier to set the options using the Prode window. All even code values mean that only single liquid phases are allowed in the flash routines. For multiple liquids, the code value must be odd.

stream 1 :

option stream mc_getOM : 554

current option set This should = 552 for stream 1 in the def.ppp archive. With this option value, only L-V flashes will result.

stream option 1 + mc_setOM 1

This changes the flashes of "stream" to multiple liquids.

stream t p mc_setOp 1

redo the flash

given a stream and phase # in range 1- getPNr() returns the phase type (0=vapor,1=liquid,2=solid)

i_1 pnr range :

given a stream and phase # in range 1- getPNr() returns a ANSI C string with the description of type for detected phase

phase i_el stream i_mc_StrPts :

phases Vapor Solid Solid Not present Not present Not present Not present Not present Not present Not present 101 mat

Previously, only one liquid was present

stream option mc_setOM 1

reset the code to single liquids

Initializing a stream

This section was changed for this version.

The example will create a stream with water and methanol. The component numbers in the Prode databank can change with updates, so always use CAS numbers when initializing by program instead of manually using the Prode window.

methanol_id 67561 :

CAS number of methanol

methanol_code methanol_id mc_CompCID : 1047

water_id 7732185 :

CAS number of water

water_code water_id mc_CompCID : 1631

stream 11 :

stream mc_initS 1

initialize a new stream

model 50 :

SRK standard

see Prode manual for model codes

stream model mc_setKM 1

set property model package

stream 1 .5 mc_putZ 1

set total stream mole fractions

stream 2 .5 mc_putZ 1

stream 1 methanol_code mc_putCC 1

define components

stream 2 water_code mc_putCC 1

stream mc_setS 1

validate the stream

codeeq =0 for VLE 1 for LLE 2 for SLE 3 for hydrates

codeeq 0 :

stream codeeq mc_loadSB 1

load BIP coefficients

stream 1.3 mc_setWm 1

set mass flow rate

temp 300 :

pres patm :

stream temp pres mc_setOp 1

set temp and pres and flash

stream mc_edS 0

view the stream then press OK

Other stream operations

stream2 1 :

stream1 10 :

stream1 stream2 mc_StrCopy 1

copy stream2 to stream1 (note the order!)

et stream2 mc_getT : 150

stream1 mc_getT 150

press stream1 mc_getP : 1.0133 105^*

stream_out 9 :

et 150

flash at lower stream press, et=temp guess for mixed stream..

stream_out stream1 stream2 press .9 * et mc_MixF 1

stream_out mc_getT 149.5844

mixed stream temperature

stream2 12 :

the new stream to be created by Divi

wdiv .7 :

stream1 stream2 wdiv mc_Divi 1

Given one stream (stream1) and a flowrate fraction (0-1) performs a divider operation so that stream 1 is shifted into two streams (stream1, stream2) of the same composition, temperature and pressure, flowrate fractions are subdivided as specified by wdiv (stream2 = wdiv, stream1 = 1- wdiv)

Only one new stream is created, NOT two.The starting stream gets overwritten as shown above.

phase separation

stream1 5 :

stream2 13 :

the new stream to be created by PSep

phase 1 :

phase number to separate, NOT the phase type

stream1 stream2 phase mc_PSep 1

Given a stream (stream1) performs an isothermal flash to simulate a phase separator and returns the specified phase number (not phase type) to stream2.

gasstream 14 :

stream1 gasstream mc_GSep 1

Given a stream (stream1) performs an isothermal flash to simulate a phase separator and returns the gas phase to gasstream

liqstream 15 :

stream1 liqstream mc_LSep 1

Given a stream (stream1) performs an isothermal flash to simulate a phase separator and returns the liq phase(s) to liqstream

Polytropic compressor/expander

rate compressor efficiency

pin 106^:

pressure in Pa

pout 2106^* :

tin 300 :

temperature in K

tout 370 :

model 2 :

for a rating, model may be the following: 2 = Huntington method 4 = Paron method

stream 2 :

stream tin pin mc_setOp 1

set the inlet stream conditions

stream pout model tout mc_PSPF 0.743

efficiency rating and "stream" in archive now contains the outlet conditions

design model

eff .75 :

polytropic efficiency given

model 1 :

for a design, model may be the following: 1 = Huntington 3 = Paron

stream tin pin mc_setOp 1

reset the inlet stream conditions

stream pout model eff mc_PSPF 369.2757

outlet temperature and "stream" now contains the outlet conditions

Isentropic expansion, nozzles

stream 5 :

pin 2106^* :

tin 340 :

stream 1.23 mc_setWm 1

stream tin pin mc_setOp 1

set stream conditions

model 2 :

model options:: 1 = homogeneous, equilibrium 2 = homogeneous, non equilibrium 3 = homogeneous, non equilibrium ? 4 = nonhomogeneous, non equilibrium

pout patm :

parameter .75 :

Prode manual does not explain this parameter

stream pout model parameter mc_ISPF 4.2071 105 -^*

calculated orifice area, m2

mc_getErrFlag 1

Pipe flow

The PIPE function is only available for users with an extended Prode license.

model 1 :

stream 1 :

diam 1 in * m / : 0.0254

rough .00045 :

length 100 km * m / : 1105^*

dHeight 0 :

dHeat 0 :

stream model diam rough length dHeight dHeat mc_PIPE 0

The result above will be 0 if the user has a Basic Prode license or 1 for an Extended license.The pressure and phase changes are made in the stream databank.

Parameters : stream (int) inlet stream model (int) model for fluid flow and phase equilibria (see below) diam (double) pipe internal diameter rough (double) parameter defining relative pipe roughness length (double) length of this segment dHeight (double) height difference (inlet, outlet) dHeat (double) heat added, removed Codes for models 1Beggs & Brill / Hazen-Williams / AGA additional models on request to Prode

File save

C:\ProgramData\prode\test.ppp mc_AFSave 1

save modifications to a new archive