View source for Example - 05 PHREEQC Projects

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== Evaporators Example ==

[[File:PHREEQC_Evap1.png]].

'''Project Location'''

..\SysCADXXX\Examples\05 PHREEQC\PHREEQCLight\Evaporators Example.spf

''' Features Demonstrated '''

#The use of [[PHREEQCModelCfg]]
#The use of [[PHREEQCEvaporator]]
#The use of [[PHREEQCFlashTank]]
 
''' Brief Project Description '''

#Each PHREEQC project must contain at least one [[PHREEQCModelCfg]] model.  There are two of these files defined here, each referencing to a different PHREEQC database.
#The PHREEQC evaporator and PHREEQC Flash Tank can both operate in standalone or [[Flash Train]] modes.  

''' Project Configuration '''

<u> [[PHREEQCModelCfg]] </u>
#The Minteq_v4 PHREEQC database is used by the standalone Evaporator and Flash tank.  
#*Note that Gypsum precipitation temperature is different to the Pitzer database (used in the flash train section)
#*The Minteq_v4 database has multiple equilibrium models, the Davies equilibrium model has been selected in our example.
#The Pitzer PHREEQC database is used by the flash train section of the model.
#*Note that Gypsum precipitation temperature is different to the Minteq_v4 database (used in the standalone section)
#*The Pitzer database does not allow multiple equilibrium models, so no selections are available.
#*SatIdx of 100 for H2O(s) has been entered in the "PHREEQCConfig" tab.
#Salts First algorithm has been selected for species re-building in both Minteq_v4 and Pitzer model configuration files.  See [[TPS Species Mapping#Reverse_Mapping|Reverse Mapping]] section for more details.

<u> PHREEQC Evaporator / Flash Tank </u>
#The configuration of the PHREEQC Evaporator / [[PHREEQCFlashTank|Flash Tank]] are very similar to the normal [[Evaporator]] and [[Flash_Tank_2|FlashTank]], the main difference is to select the PHREEQC Chemistry model to be used.

== RO Plant Example ==

[[File:PHREEQC_RO1.png]] .

'''Project Location'''

..\SysCADXXX\Examples\05 PHREEQC\PHREEQCLight\RO Plant Example.spf

''' Features Demonstrated '''

#The use of [[PHREEQCModelCfg]]
#The use of [[PHREEQCReverseOsmosis]]
 
''' Brief Project Description '''

#Each PHREEQC project must contain at least one [[PHREEQCModelCfg]] model.  
#This project demonstrates the use of the RO unit for calculating max permeate recovery. 
#Influence of antiscalant. This is modelled by creating a second PHREEQC configuration where we allow supersaturation of gypsum.  The concentrate RO skid (RO6) uses this configuration in its calculation of maximum permeate recovery.

''' Project Configuration '''

<u> [[PHREEQCModelCfg]] </u>
#The Minteq_v4 PHREEQC database is used by the RO 01 to 05 units.  
#*The Minteq_v4 database has multiple equilibrium models, the Davies equilibrium model has been selected in our example.
#A second Minteq_v4 PHREEQC database is used by the RO 06 unit to emulate the influence of antiscalant.
#*SatIdx of 0.3 for CaSO4:2H2O(s)(Gypsum) and CaSO4(s) have been entered in the "PHREEQCConfig" tab.
#Salts First algorithm has been selected for species re-building in both Minteq_v4 and Pitzer model configuration files.  See [[TPS Species Mapping#Reverse_Mapping|Reverse Mapping]] section for more details.

<u> [[PHREEQCReverseOsmosis]] </u>
#The configuration of the [[PHREEQCReverseOsmosis]] is similar to the normal [[Reverse Osmosis (RO) Unit]], the main difference are:
#* select the PHREEQC Chemistry model to be used and 
#*model method: MaxYield for maximum permeate recovery.

== Simple Reactor Example ==

[[File:PHREEQC_Reactor1.png]]

'''Project Location'''

..\SysCADXXX\Examples\05 PHREEQC\PHREEQCLight\Simple Reactor Example.spf

''' Features Demonstrated '''

#The use of [[PHREEQCModelCfg]]
#The use of [[PHREEQCReactor]]
#The use of [[PHREEQCSideCalc]] 

''' Brief Project Description '''

In this demo project, we demonstrate several different operating modes for the PHREEQC reactor.
#Isenthalpic, temperature of the output is calculated for an acid-base reaction
#Isothermal, temperature is set to the temperature of the incoming stream mixture, heat flow required to achieve this is calculated
#A temperature setpoint is set, heat loss is also incorporated
#This tank is linked with a side calculation.  The side calculation is doing a calculation to determine the water required to dissolve the gypsum coming in to the tank.  The calculated water flow is then applied to the makeup of the actual reactor tank.  This demonstrates a feed-forward control strategy for water addition
#Each PHREEQC project must contain at least one [[PHREEQCModelCfg]] model. 
#*We have used two [[PHREEQCModelCfg]] models in this project, one we allow supersaturation of gypsum.

''' Project Configuration '''

<u> [[PHREEQCModelCfg]] </u>
#The Minteq_v4 PHREEQC database is used by the PR_001, PR_002 and PR_004 units.  
#*The Minteq_v4 database has multiple equilibrium models, the Davies equilibrium model has been selected in our example.
#A second Minteq_v4 PHREEQC database is used by the PR_003 unit to emulate the Gypsum being supersaturated.
#*SatIdx of 0.1 for CaSO4:2H2O(s)(Gypsum) has been entered in the "PHREEQCConfig" tab.
#Salts First algorithm has been selected for species re-building in both Minteq_v4 and Pitzer model configuration files.  See [[TPS Species Mapping#Reverse_Mapping|Reverse Mapping]] section for more details.

<u> [[PHREEQCReactor]] </u>
#PR_001
#*Ca(OH)2 addition is being constrained, this is done by ticking "UseCFE" and in the CFE tab: Ca(OH)2 has 5% inert fraction.
#*Calculation mode is isenthalpic (delta enthalpy = 0 kW)
#*We found gypsum precipitation occurs and a slight pickup in tank temperature due to reaction. There are some Ca(OH)2 remaining due to the user specified inert fraction
#PR_002
#*Calculation mode is isothermal (Final T = Feed T), heat flow required to achieve this is shown in the PHREEQCResults, Energy balance section.
#*Ca(OH)2 addition is fully used and gypsum precipitation occurred
#PR_003
#*Calculation mode is user specified temperature,  heat flow required to achieve this is shown in the PHREEQCResults, Energy balance section.
#*This reactor also uses a different SatIdx for gypsum, allowing gypsum to be supersaturated.
#*Heat loss is also being used in this model.
#PR_004 and PSC_001
#*The PSC_001 has been set up to determine the water required to dissolve the gypsum coming in to PR_004.  The calculated water flow is then applied to the makeup of the actual reactor tank.  This demonstrates a feed-forward control strategy for water addition. 

== USX Example ==
[[File:PHREEQC_USX1.png]] [[File:PHREEQC_USX2.png]]

'''Project Location'''

..\SysCADXXX\Examples\05 PHREEQC\PHREEQCFull\USX Example.spf

{{Available139|30918}}

''' Features Demonstrated '''

#The use of [[PHREEQC Overview|PHREEQC]] Thermodynamic Calculation Engine using a customised database.
#The use of [[PHREEQC Model Configuration]].
#The use of [[PHREEQC Solvent Extraction]].
#The use of [[PHREEQC Side Calc Model]].
#The use of [[Solvent Extraction Unit|Solvent Extraction (Mixer/Settler) Unit]] with an isotherm.
#The use of the [[Feeder-Cross_Page_Connector#Feeder_Operation_Selection|Stream Fetch]] operation in a [[Feeder-Cross Page Connector|Feeder]].
#The use of [[Makeup Source|Makeup Sources]] and [[Makeup Block (MU)|Makeup Blocks]].
#The use of the [[Discard Sink]] and [[Discard Block (DB)|Discard Block]].
#The use of [[Reactions]], including reaction override.
#The use of a [[General Controller]].
#The use of a [[Set Tag Controller]].
#The use of a [[PID Controller]].

''' Brief Project Description '''

*This example project was used as the basis for a paper entitled [[Media:HEPPNER - ALTA 2022.pdf|''"First Principles Modelling of the Solvent Extraction and Stripping of Uranium including Molybdenum Control"'']], which was presented at ALTA 2022 in Perth by Kevin Heppner.
*This is a simplified model of a uranium solvent extraction (USX) plant.  It is a typical plant arrangement with extraction, strong acid stripping, and organic regeneration.  It is not intended to model any particular plant.
*The PHREEQC minteq.v4.dat model is used with the addition of chemistry to account for extraction of molybdenum, acid, and uranium to tertiary amine.  The chemistry model was fitted to data in the open literature:
**N Yakabu and A Dudeney, “A study of uranium solvent extraction equilibria with Alamine 336 in kerosene”, Hydrometallurgy, 1987
**J. Coca, F. Diez, and M Moris, “Solvent extraction of molybdenum and tungsten by Alamine 336 and DEHPA”, Hydrometallurgy 1990.
*[[Feeder-Cross_Page_Connector#Feeder_Operation_Selection|Stream Fetch]] is used to model the recirculating organic stream. The composition of the returning barren organic is fetched by the feeder to the extraction circuit.
*Pregnant aqueous solution is fed to the extraction circuit.  The concentration of uranium, molybdenum, and free acid can be set in the General Controller on the extraction flowsheet.
*The uranium is extracted in four extraction stages, each modelled using PHREEQC mixer settler units.  Molybdenum is also coextracted.  The extent of extraction is determined by PHREEQC thermodynamic calculations.
*The loaded organic is scrubbed using dilute acid.  This is again modelled using a PHREEQC mixer settler unit.  The aqueous is sent to extraction cell 1 and the scrubbed organic continues on to stripping.
*The scrubbed, loaded organic is stripping using strong acid solution over a series of 7 stripping stages.  The extent of stripping is determined by a strong acid stripping isotherm obtained from literature:
**C.A. Morais , L.A. Gomiero , W. Scassiotti Filho , H. Rangel Jr., “Uranium stripping from tertiary amine by sulfuric acid solution and its precipitation as uranium peroxide”, Minerals Engineering, 2005.
*A portion of the stripped organic is washed with water to recover excess acid.  The washing process is modelled using a PHREEQC mixer settler unit.  The washed organic is then sent to regeneration.
*The washed organic is regenerated with a dilute solution of sodium carbonate to remove all metals from the amine. A PHREEQC side calculation is used to calculate the pH of the spent regeneration solution. The regenerated organic is combined with the portion of the organic which was not washed or regenerated in the barren organic tank.
*Organic diluent and tertiary amine are added to the barren organic tank via makeups.  The makeups are controlled as follows:
**Tertiary amine is added to maintain a target percentage amine in the barren organic
**Organic diluent is added so that the flow of barren organic leaving the stripping page exactly matches the flow of organic fed to extraction
**Combined with stream fetch of the extraction organic feed stream, the above is an implementation of a tear on the recirculating organic stream which greatly improves overall model convergence.

''' Project Configuration '''

*Most units with reactions are simulated by the PHREEQC mixer settler and mixer settler unit operations.
*Makeup Blocks are used:
**in the Strip Solution Tank to achieve a target acid concentration for feed solution to stripping
**in the Barren Organic Tank to achieve a target amine concentration
**in the Barren Organic Tank to achieve a target product flow
*PID Controllers are used to regulate the addition of sodium carbonate to the regeneration cell (based upon the calculated pH from the PHREEQC side calculation).
*A General Controller is used to perform a number of calculations and to provide an input/output summary for key input parameters and key performance indicators.
*A General controller is also used to calculate the required organic diluent makeup/discard and match the extraction circuit feed flow (to close the organic mass balance).
*PID and SetTag controllers are used to vary the Regen Solution flow (sodium carbonate solution) to the Regeneration Cell to meet the pH target (based upon the calculated pH from the PHREEQC side calculation).
*A PID controller is used to vary the wash water flow to the Wash Cell to produce the required Strip Solution flow to achieve the target advance O:A ratio in the stripping circuit.

'''Included Excel Report'''

PHREEQC USX Example Report.xlsx

This file has the following reports:
*Criteria
*Streams
*Mass Balance

== Raffinate Water Treatment Example ==
[[File:Raffinate_Treatment_Demo.png]]

'''Project Location'''

..\SysCADXXX\Examples\05 PHREEQC\PHREEQCFull\Raffinate Treatment Example.spf

{{Available139|32067}}

''' Features Demonstrated '''

#The use of [[PHREEQC Overview|PHREEQC]] Thermodynamic Calculation Engine.
#The use of [[PHREEQC Model Configuration]].
#The use of [[PHREEQC Reactor]].
#The use of [[PHREEQC Side Calc Model]].
#The use of [[General Separator]].
#The use of [[Makeup Source|Makeup Sources]] and [[Makeup Block (MU)|Makeup Blocks]].
#The use of a [[General Controller]].
#The use of a [[PID Controller]].

''' Brief Project Description '''

*This is a simplified model of a raffinate water treatment plant.  It is a typical plant arrangement with two stage treatment at low and high pH, followed by tailings thickening.  It is not intended to model any particular plant.
*The PHREEQC minteq.v4.dat model is used.
*Raffinate wastewater solution is fed to the low pH treatment tank.
*The water is purified in two stages of ferric sulphate and lime addition.  The extent of reaction is determined by PHREEQC thermodynamic calculations.
*The tailings are treated in a series of tailings treatment tanks, with the product tailings sent to a thickener.
*The tailings thickener overflow is recycled to the feed of the low pH treatment tank.
*Each clarifier recycles a portion of its underflow back to the tank of its treatment circuit, which is common practice in water treatment to promote better solids settling.

''' Project Configuration '''

*Most units with reactions are simulated by the PHREEQC Reactor in constant enthalpy mode.
*Makeup Blocks are used:
**for addition of ferric sulphate (based upon mass ratios for addition)
**for addition of lime slurry
*PID Controllers are used to control the pH of all tanks in the process by the addition of lime
*General Controllers are used to perform a number of calculations and to provide a calculation of removal efficiency for some selected metals.
*Annotation tables are used to report key performance indicators for the plant directly on the flowsheet.
<!--
== Potash Crystallisation Example Project ==

[[Image:PHREEQC_Full_PotashExample.png]]

'''Project Location'''

This is a Steady State project and is stored at:

..\SysCADXXX\Examples\06 PHREEQC\PHREEQCFull\Potash_Crystallisation.spf

{{Available139|XXXXX}}

''' Features Demonstrated '''

# The Use of [[PHREEQC Model Configuration]] - with a PHREEQC database file (pitzer.dat).
# Setting up flash trains using [[PHREEQC Evaporator]] with [[Shell_and_Tube_Heat_Exchanger_2|Shell and Tube Heat Exchanger 2]] & [[Barometric Condenser]].

NOTE: This is similar to the [[Example_Potash_Projects#Four_Stage_Crystallisation_Example_Project|Potash example project]], but instead of using the Potash add-on, it is using the PHREEQC Solver.

''' Brief Project Description '''

:*This is a MOP (Muriate of Potash) example project.
:*This project shows a 4-Stage-Evaporator(crystalliser) circuit.
:*This project uses constant feed for Liquor Feed and Brine streams.
:*Crystallisation is based on PHREEQC solver solution.
:*Dilution water is added to each crystallisation stage.
:*PotashEvaporator underflow (crystallised material) is removed from the first third and fourth stage.  Second stage underflow is feed to the 3rd stage.
:*Brine is used to exchange heat in the Barometric condensers.

'''Project Configuration'''

<u> [[PHREEQC Model Configuration]] </u>
:*The potash.dbs database is used.  This is generated using the PHREEQC MSE framework.

<u>''PHREEQC Evaporator''</u>
:*PHREEQCEvaporator Tab
:#Select FlashTrain mode 
:#Specify minimum flash temperature for the unit (this will assist with pressure balance of the circuit)
:#Set up the TCE tab page - use "Potash_PHREEQC" 
:#Set up the Separ tab page - required Overflow and Underflow sPHREEQCds.
:#Set up dilution water to the crystalliser.

<u>''Barometric Condenser''</u>
:*Set the approach temperature.

<u>''Shell and Tube Heat Exchange''</u>
:*HX_001 is used to condense the flash steam from the 1st Crystalliser, 
:#Method - CondensingSteam 
:#Condensing Method: Demand (UA) 
:#Demand Connection: FlashTrain
:#The condenser area and HTC information is supplied. 
:*HX_002 is used to preheat the feed with recycle Brine
:#Method - Sensible HX
:#The heater area and HTC information is supplied.
-->
== Raffinate Water Treatment Example With Adsorption ==
[[File:Raffinate_Water_Treatment_with_Adsorption2.png|800px]]

'''Project Location'''

..\SysCADXXX\Examples\05 PHREEQC\PHREEQCFull\Raffinate Treatment (Adsorption) Example.spf

{{Available139|34461}}

''' Features Demonstrated '''

#The use of [[PHREEQC Overview|PHREEQC]] Thermodynamic Calculation Engine.
#The use of [[PHREEQC Model Configuration]].
#The use of [[PHREEQC Reactor]].
#The use of [[PHREEQC Feeder Model]].
#The use of [[General Separator]].
#The use of [[Makeup Source|Makeup Sources]] and [[Makeup Block (MU)|Makeup Blocks]].
#The use of [[Discard Sink]] and [[Discard Block (DB)|Discard Blocks]].
#The use of a [[General Controller]].
#The use of a [[PID Controller]].

''' Brief Project Description '''

*This is a simplified model of a raffinate water treatment plant.  It is a typical plant arrangement with two stage treatment at low and high pH, followed by tailings thickening.  It is not intended to model any particular plant.
*This model is very similar to the [[#Raffinate_Water_Treatment_Example|raffinate water treatment plant example project]], but using a different configuration file.
*The PHREEQC minteq.v4.syscad_alumina.dat model is used.  It utilizes the minteq.v4 database with additional data on alumina sorption obtained from open literature sources.
*Raffinate wastewater solution is fed to the low pH treatment tank.
*The water is purified in two stages of ferric sulphate, lime and air addition.  The extent of reaction is determined by PHREEQC thermodynamic calculations.
*The tailings are treated in a series of tailings treatment tanks, with the product tailings sent to a thickener.
*The tailings thickener overflow is recycled to the feed of the low pH treatment tank.
*Each clarifier recycles a portion of its underflow back to the tank of its treatment circuit, which is common practice in water treatment to promote better solids settling.

''' Project Configuration '''

*The Raffinate feed is specified using a PHREEQC Feeder.
*Most units with reactions are simulated by the PHREEQC Reactor in constant enthalpy mode.
*Makeup Blocks are used:
**for addition of ferric sulphate (based upon mole ratios for addition)
**for addition of lime slurry (mass ratios or mass flows set by PID controllers)
**for addition of air (fixed volumetric flow)
*Discard Blocks are used to remove vapours from the pH treatment tank outlets
*PID Controllers are used to control the pH of all tanks in the process by the addition of lime
*General Controllers are used to perform a number of calculations and to provide a calculation of removal efficiency for some selected metals.
*Annotation tables are used to report key performance indicators for the plant directly on the flowsheet.
*The adsorption model in the SysCAD PHREEQC interface is used.  This allows calculation of the competitive adsorption of dissolved metals alongside co-precipitation of sparingly soluble salts and metal oxyhydroxides.
*Adsorption extent is determined from the amount of ferric and alumina precipitates generated in the reactions.
*This model was presented at MetPlant 2023.  Please request paper for more information.

'''Included Excel Report'''

Sensitivity Analysis.xlsm

The file used and its associated macros are described here: [[Sensitivity Analysis]]. It has been customised for this project.

== REE SX Example ==

[[File:REE_SX1.png|800px]] [[File:REE_SX2.png|800px]] [[File:REE_SX3.png|800px]] [[File:REE_SX4.png|800px]][[File:REE_SX0.png|800px]]

'''Project Location'''

..\SysCADXXX\Examples\05 PHREEQC\PHREEQCFull\REE SX Example.spf

Project updated in {{Available139|36450||y}} to include the Summary flowsheet.

''' Features Demonstrated '''

#The use of [[PHREEQC Overview|PHREEQC]] Thermodynamic Calculation Engine using a customised database.
#The use of [[PHREEQC Model Configuration]].
#The use of [[PHREEQC Solvent Extraction]].
#The use of the [[Feeder-Cross_Page_Connector#Feeder_Operation_Selection|Stream Fetch]] operation in a [[Feeder-Cross Page Connector|Feeder]].
#The use of the [[PGM_Example_-_Relaxed_Cross_Page_Connector|PGM class for relaxed fetch]] operation in a [[Feeder-Cross Page Connector|Feeder]].
#The use of [[Makeup Source|Makeup Sources]] and [[Makeup Block (MU)|Makeup Blocks]].
#The use of the [[Discard Sink]] and [[Discard Block (DB)|Discard Block]].
#The use of a [[General Controller]].
#The use of a [[PID Controller]].
#The use of [[User Property Calculations]].

''' Brief Project Description '''

*This example project was used as the basis for a paper entitled <!-- [[Media:SCHUG_HEPPNER - ALTA 2024.pdf|''"Thermodynamic Modelling of Rare Earth Solvent Extraction"'']]-->"Thermodynamic Modelling of Rare Earth Solvent Extraction", which was presented at ALTA 2024 in Perth by Brett Schug.
*This is a model of a typical rare earth solvent extraction circuit.  It is a typical plant arrangement with extraction, scrubbing, stripping, and saponification.  It is not intended to model any particular plant.
*It includes a heavies removal circuit, which represents the balance of plant as a black box to restore organic a mixture of acidified and saponified organic without heavy element recycle.
*The PHREEQC pitzer.dat model is used with the addition of chemistry to account for extraction of La, Ce, Pr, Nd, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, Lu, and Y.  All data is obtained from open literature sources, see "References" below.

*[[PGM_Example_-_Relaxed_Cross_Page_Connector|PGM class for relaxed fetch]] is used to model the recirculating organic stream. The composition of the returning barren organic is fetched by the feeder to the extraction circuit.  The update of composition is relaxed to enhance convergence.
*Pregnant aqueous solution is fed to the extraction circuit.  The concentration of La, Ce, Pr, Nd, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, Lu, and Y can be set in the General Controller on the extraction flowsheet.
*The REE elements are extracted in up to 36 extraction stages, each modelled using PHREEQC mixer settler units.  The extent of extraction is determined by PHREEQC thermodynamic calculations.
*The loaded organic is scrubbed using a portion of the loaded strip which is refluxed from the stripping circuit.
*The scrubbed, loaded organic is stripping using strong acid solution over a series of up to 4 stripping stages.
*The barren organic leaving stripping reports to a heavies strip black box process.  Here, excess acid is added to ensure all remaining REE elements are removed.
*The cleaned organic leaving REE is saponified using NaOH.
*The cleaned, saponified organic is recycled back to the extraction circuit, thus completing the organic recirculation cycle.
*Organic diluent and PC88A extractant are added to the barren organic tank via makeups.  The makeups are controlled as follows:
**PC88A extractant is added to maintain a target percentage amine in the barren organic
**Organic diluent is added so that the flow of barren organic leaving the stripping page exactly matches the flow of organic fed to extraction
**Combined with stream fetch of the extraction organic feed stream, the above is an implementation of a tear on the recirculating organic stream which greatly improves overall model convergence.

''' Project Configuration '''
*Most units with reactions are simulated by the PHREEQC mixer settler and mixer settler unit operations.
*Makeup Blocks are used:
**in the Barren Organic Tank to achieve a target extractant concentration
**in the Barren Organic Tank to achieve a target product flow
*PID Controllers are used to regulate the addition of sodium hydroxide to the saponification tank (based upon the calculated saponification extent from the PHREEQC calculation in that tank).
**Saponification extent is defined as: <math> SE=\frac{Moles_PC88A-Na}{Total_Moles_PC88A} </math>
*A General Controller is used to turn on/off cells in each area of the circuit based upon the user-defined number of cells.  Cells have a maximum count of:
**36 extraction cells
**36 scrubbing cells
**4 stripping cells
*A General Controller is used to perform a number of calculations and to provide an input/output summary for key input parameters and key performance indicators.
*A General controller is also used to calculate the required organic diluent makeup/discard and match the extraction circuit feed flow (to close the organic mass balance).
*A [[PGM_Example_-_Relaxed_Cross_Page_Connector|PGM class for relaxed fetch]] is used to couple two [[Feeder-Cross Page Connector|Feeders]] using a relaxed fetch algorithm.  This is useful for difficult to converge systems such as the REE SX model.

'''Included Scenarios'''

{{Available139|36450}}

Two scenario files are included in the project.  
*"Scn_Full_25E_15Sc_4St_30Sap.scn" - The project is configured according to the original Alta 2024 paper, with pregnant liquor including all REEs and a large number of extraction and scrubbing stages. This full version takes a considerable amount of time to solve due to its complexity.
*"Scn_Simple_10E_10Sc_4St_29Sap.scn" -The project is configured with pregnant liquor including only three REEs and fewer extraction and scrubbing stages. This simplified version can be used to test key concepts as it solves much faster than the full project.
*Use Project - Load Scenario to load the appropriate case before solving.

'''Included Excel Report'''

SX Profiles.xlsx

This file has the following reports:
*Criteria
*Streams
*Mass Balance
*Various reports showing distribution of all REEs across the stages of the circuit
**These demonstrate more sophisticated [[Excel_Tag_Select_Reports|Excel Tag Select Reports]] to, for example, create a list of all organic streams in the correct order to allow plotting of the profiles
*A report showing the distribution of each REE to each exiting stream

'''References'''
#Lyon, K.L., Utgikar, V.P., Greenhalgh, M.R., 2017. Dynamic Modeling for the Separation of Rare Earth Elements Using Solvent Extraction: Predicting Separation Performance Using Laboratory Equilibrium Data. Ind. Eng. Chem. Res., 56 (2017) pp. 1048 – 1056.
#Zhang, Y., Gu, F., Su, Z., Liu, S., Anderson, C., Jiang, T., 2020. Hydrometallurgical Recovery of Rare Earth Elements from NdFeB Permanent Magnet Scrap: A Review. Metals, Vol. 10, p. 841; doi:10.3390/met10060841
#Simoes, M.C., Hughes, K.J., Ingham, D.B., Ma., L., Pourkashanian, M., 2016. Estimation of the Pitzer Parameters for 1–1, 2–1, 3–1, 4–1, and 2–2 Single Electrolytes at 25 °C. Journal of Chemical & Engineering Data, Vol. 61, No. 7, pp. 2536-2554.
#Simoes, M.C., Hughes, K.J., Ingham, D.B., Ma., L., Pourkashanian, M., 2017. Temperature Dependence of the Parameters in the Pitzer Equations. Journal of Chemical & Engineering Data, Vol. 62 No. 7 (2017) pp. 2000-2013.
#Turgeon, K., Boulanger, J-F., Bazin, C., 2023. Simulation of Solvent Extraction Circuits for the Separation of Rare Earth Elements. Minerals, 13, 714
#Roy, R.N., Roy, L.N., Tabor, B.J., Himes, C.A., Richards, S.J., Cummins, M.P., Christiansen, E.B., Roy, C.N., Sharma, V.K., Millero, F.J., 2005. Thermodynamics of Electrolyte Mixtures: HCl + NdCl3 + H2O from 5 to 55°C. Journal of Solution Chemistry, Vol. 34, No. 9, 1033–1044.
#Pitzer, K.S., Mayorga, G., 1973. Thermodynamics of Electrolytes. II. Activity and Osmotic Coefficients for Strong Electrolytes with One or Both Ions Univalent. The Journal of Physical Chemistry. Vol. 77, No. 19, pp. 2300 – 2308.
#Zaki, E.E, Ismail, Z.H., Sabet, S.A., Aly, H.F., 2020. Equilibrium Studies on the Extraction of Yttrium from Chloride Medium by Mono (2-Ethylhexyl) 2-Ethylhexyl Phosphonic Acid. Report #EG0800276, Preprint, Mar 2020.
#Pitzer.dat database, distributed with PHREEQC
#LLNL.dat database, distributed with PHREEQC