Desalination Economic Evaluation Program
Contents
1. m d C C C ppm 1 m hour Lost Electricity Production Power to Heat Ratio Plant Thermal Utilization Distillation Performance of Effects Stages GOR Temperature Range Distillate Flow Feed Flow Steam Flow Brine Flow Brine salinity Specific Heat Consumption 20 0 1 7 75 5 9 8 0 20 100 000 200 000 144 39 100 000 70 000 80 67 MW MWe MWt C kg s ppm kWh m RO Performance Recovery Ratio Permeate Flow Feed Flow Feed Pressure Product Quality Brine Flow Brine Saliniy Specific Power Consumption N A N A N A N A N A N A N A N A bar ppm ppm kWh Specific Power Costs Fixed charge cost Fuel cost O amp M cost Decommissioning cost Levelized Electricity Cost 0 008 0 075 0 006 N A 0 088 kWh kWh kWh kWh kWh Specific Water Costs Fixed charge cost Heat cost Plant electricity cost Purchased electricity cost O amp M cost Total Specific Water Cost 0 328 0 424 0 204 0 000 0 139 1 093 m m m m m m 19 20 Project Power Plant Data Type Ref Thermal Power Ref Net Electric Power Construction Cost Fuel Cost Purchased Electricity Cost Interest Rate Configuration Switches Steam Source Intermediate Loop TVC Option Backup Heat RO Energy Recovery Device Summary o2. DPhm High head pump pressure rise EN CENE CUT NR Ehm pump copingeficieny i y O Qsom joterspeoficpoweruse Nem om Planned outagerate ____ 1 __ oum unplanned outagerate o o o o if O value is calculated Ampo Plant availability RO Plant Cost Data BUM Variable Description Unit Default Remarks RO plant base unit cost a a o LUE Plant owners costfactor _ _ E tmo Plant avaitabiity PO vaueiscaedoted Smm average management salary o Sm average taborsalary emm oammembranereplacementcost sim emp foam spare partscost omor Specific chemicals costfor pretreatment sim _ mopo Specific chemicals cost for posttreatment km imtosminsuranceoost mf Nmmo _ of management personnel valets calculated Number ofaborpersonnel J _ __ Hybrid Plant Data Input Variable Description Unit Default Remarks Required total desalination capacity 0002 dist capacity O We __ Hybrid RO capacity fo iho Hybrid lant lead time EK ME 17 6 2 Output sheet Performance Results Description Unit Remarks Lost Electricity Production MW Power to Heat Ratio Plant Thermal Utilization Distillation Performance Description Unit of Effects Stag
3. 273 10 Where T extracted steam C Note that the cases involving available waste heat such as gas cooled reactors correspond to a backpressure configuration with Which implies free available heat and no lost shaft work For the backup pressure cases the heating steam is limited by the heat exchanger or con denser load For extraction cases it is limited by the available heat source The following ex pression is used lt Qi QJ 1 n 11 Where refers to the available thermal power and refers to the produced electric power 4 2 RO performance model The flow chart for the Reverse Osmosis RO model is shown in Fig 7 Recovery ration Estimate Product Flow amp Quality Estimate Feed Flow amp Pressure Estimate Pumping Power Requirements Fig 7 Flowchart for RO performance model Here again the user can either specify the system recovery ratio or have it estimated by DEEP as follows 1 CNS S 12 Where Sr refers to the feed salinity in ppm and is a constant defined as CNS 1 15E 3 P max 13 refers to the maximum design pressure of the membrane in bars Note that as feed salinity becomes small the recovery ratio approaches unity and as it ap proaches the numerical equivalent of maximum membrane pressure in millibars recovery goes to zero as would be expected in practice For permeate salinity and feed pressure we use the expressions give
4. Power plant MEE product water Back pressure steam turbine Seawater feed Low pressure steam Blended product water 0 34 bar 70 C seawater Preheated makeup seawater Concentrate discharge Concentrate Pre heated feed Product water RO product Energy water recovery turbine Fig 2 Sketch of hybrid MED RO layout 2 1 Multi stage flash MSF distillation Figure 2 shows the schematic flow diagram of an MSF system Seawater feed passes through tubes in each evaporation stage where it is progressively heated Final seawater heating occurs in the brine heater by the heat source Subsequently the heated brine flows through nozzles into the first stage which is maintained at a pressure slightly lower than the saturation pres sure of the incoming stream As a result a small fraction of the brine flashes forming pure steam The heat to flash the vapour comes from cooling of the remaining brine flow which lowers the brine temperature Subsequently the produced vapour passes through a mesh de mister in the upper chamber of the evaporation stage where it condenses on the outside of the condensing brine tubes and is collected in a distillate tray The heat transferred by the conden sation warms the incoming seawater feed as it passes through that stage The remaining brine passes successively through all the stages at progressively lower pressures where the process is repeated The hot distillate
5. 0 088 kWh kWh kWh kWh kWh Specific Water Costs Fixed charge cost Heat cost Plant electricity cost Purchased electricity cost O amp M cost Total Specific Water Cost 0 301 0 195 0 213 0 007 0 158 0 873 m m m m m m Summary of Performance and Cost Results Main Input Parameters Water Plant Data Required capacity Hybrid Dist Capacity Dist Construction Cost Maximum Brine Temp Heating Steam Temp Project DEEP Version 3 0 Sep 2005 Power Plant Data Type NBC Type Ref Thermal Power 1 570 MW Ref Net Electric Power 660 MW Construction Cost 1 500 kW Fuel Cost 6 MWh Purchased Electricity Cost 0 06 S kWh Interest Rate 5 Configuration Switches Steam Source ExtrCon Intermediate Loop Y TVC Option N Backup Heat N RO Energy Recovery Device PEX Dist Feed Temp Seawater Feed Salinity Hybrid RO Capacity RO Construction Cost RO Recovery Ratio RO Energy Recovery Efficiency RO Design Flux RO Feed Temp Case MED RO 100 000 50 000 900 65 0 0 0 30 35000 0 50 000 900 0 00 0 95 13 6 30 0 NBC MED RO m d C C C ppm m d 1 m hour C Lost Electricity Production 0 0 MW Power to Heat Ratio 3 9 MWe MWt Plant Thermal Utilization 52 4 96 Distillation Performance of Effects Stages 9 GOR 8 0 Temperature Range 20 C Distillate Flow 50 000 4 Feed Flow 100 000 m d Steam Flow 722
6. COMPUTER MANUAL SERIES No 19 Desalination Economic Evaluation Program DEEP 3 0 User s Manual 5 IAEA International Atomic Energy Agency COMPUTER MANUAL SERIES No 19 Desalination Economic Evaluation Program DEEP 3 0 User s Manual INTERNATIONAL ATOMIC ENERGY AGENCY VIENNA 2006 The originating Section of this publication in the IAEA was Nuclear Power Technology Development Section International Atomic Energy Agency Wagramer Strasse 5 P O Box 100 A 1400 Vienna Austria DESALINATION ECONOMIC EVALUATION PROGRAM DEEP 3 0 IAEA VIENNA 2006 IAEA CMS 19 IAEA 2006 Printed by the IAEA in Austria April 2006 FOREWORD DEEP is a Desalination Economic Evaluation Program developed by the International Atomic Energy Agency IAEA and made freely available for download under a license agreement www iaea org nucleardesalination The program is based on linked Microsoft Excel spreadsheets and can be useful for evaluating desalination strategies by calculating estimates of technical performance and costs for various alternative energy and desalination technology configurations Desalination technology options modeled include multi stage flashing MSF multi effect distillation MED reverse osmosis RO and hybrid options RO MSF RO MED while energy source options include nuclear fossil renewables and grid electricity stand alone RO Version 3 of DEEP DEEP 3 0 features important changes fr
7. the thermal and RO models described above 4 4 Cost model Cost calculations in DEEP are done for both power and water plants and are case sepcific Capital costs as well as fuel operation and maintenance and other costs are taken into consid eration Water capacity scaling is taken into account in cost calculations if specified by the user DEEP uses the power credit method 9 to estimate the value of steam in co generation sys tems The essence of this method is that the cost of the low pressure steam per unit vol ume of produced water is determined by the lost value of the additional electric power KWh which could have been produced instead This is sometimes alternatively referred to as the lost shaft work C Ce AQUW 18 Where C is the base electricity cost per KWh and W is the volumetric water production rate per hour While there are other methods available for high power to water ratios the power credit method is considered adequate S DEEP 3 0 PROGRAM INSTRUCTIONS The DEEP programme structure is based on the linking of macro enabled Excel spreadsheets The linking procedure enables the separation of the calculation and presentation parts of the software Performance and cost estimates of co generated electricity and water or alternatively water for water only plants are calculated by the programme engine DEEP xls and saved in sepa rate case files under the User Files Cases subfolder In the pr
8. 0 kg s Brine Flow 50 000 m d Brine salinity 70 000 ppm Specific Heat Consumption 80 67 kWh m RO Performance Recovery Ratio Permeate Flow Feed Flow Feed Pressure Product Quality Brine Flow Brine Saliniy Specific Power Consumption 0 42 50 000 120 000 56 1 279 70 000 60 000 2 91 bar ppm ppm kWh m Specific Power Costs Fixed charge cost 0 013 kWh Fuel cost 0 009 kWh O amp M cost 0 012 S KkWh Decommissioning cost 0 004 S KkWh Levelized Electricity Cost 0 037 kWh Specific Water Costs Fixed charge cost Heat cost Plant electricity cost Purchased electricity cost O amp M cost Total Specific Water Cost 0 311 0 000 0 097 0 006 0 157 0 571 m m m m m m 21 22 Summary of Performance and Cost Results Project Power Plant Data Type Ref Thermal Power Ref Net Electric Power Construction Cost Fuel Cost Purchased Electricity Cost Interest Rate Configuration Switches Steam Source Intermediate Loop TVC Option Backup Heat RO Energy Recovery Device N A N A N A N A N A 0 037 N A N A N A PEX MW MW kW MWh S kWh DEEP Version 3 0 Sep 2005 Water Plant Data Type Required capacity Hybrid Dist Capacity Dist Construction Cost Maximum Brine Temp Heating Steam Temp Dist Feed Temp Seawater Feed Salinity Hybrid RO Capacity RO Construction Cost RO Recovery Ratio RO Energy Recover
9. 6 DEEP 3 0 INPUT OUTPUT DESCRIPTION 14 6 1 Input sheet isses p Seah e E ite die 14 6 2 Output sheet ee rem t oed bei t a ee a 18 JT 3 0 SAMPEE CASES 5 rnt FU pd rires 19 ME EE TM 23 CONTRIBUTORS TO DRAFTING AND 25 1 INTRODUCTION Desalination is known to be an energy intensive process requiring mainly low temperature steam for distillation and high pressure pumping power for membrane systems Traditionally fossil fuels such as oil and gas have been the major energy sources However fuel price hikes and volatility as well as concerns about long term supplies and environmental release is prompting consideration of alternative energy sources for sewater desalination such as nuclear desalination 1 and the use of renewable energy sources 2 If we add to this the fact that the coupling methods between power and desalination units can also vary the need for a performance and cost analysis tool to assist in design selection and optimization becomes clear The Desalination Economic Evaluation Program DEEP is a spreadsheet tool originally developed for the IAEA by General Atomics 3 and later expanded in scope by the IAEA in what came to be known as the DEEP 2 version 4 Recently the models have been thoroughly reviewed and upgraded and a ne
10. aturated steam is used which is supplied by steam boilers or dual purpose plants co generation of electricity and steam b Cooling Seawater Feed Seawater Distillate Brine Blow Down Fig 4 Sketch of MED layout Currently MED processes with the highest technical and economic potential are the low tem perature horizontal tube multi effect process LT HTME and the vertical tube evaporation process VTE In LT HTME plants evaporation tubes are arranged horizontally and evaporation occurs by spraying the brine over the outside of the horizontal tubes creating a thin film from which steam evaporates In VTE plants evaporation takes place inside vertical tubes 2 3 MED plants with vapour compression VC In some MED designs a part of the vapour produced in the last effect is compressed to a higher temperature level so that the energy efficiency of the MED plant can be improved va pour compression To compress the vapour either mechanical or thermal compressors are used 2 4 Reverse osmosis RO Reverse osmosis is a membrane separation process in which pure water is forced out of a concentrated saline solution by flowing through a membrane at a high static transmembrane pressure difference This pressure difference must be higher than the osmotic pressure be tween the solution and the pure water The saline feed is pumped into a closed vessel where it is pressurised against the membrane A
11. costing models the coupling configuration matrix and the user interface as well as a thorough review of the configuration templates The thermal model upgrade includes 1 A generalization of the lost shaft work to model both extraction and backpressure coupling configurations 2 Improvements in the distillation thermal balance model and Gain Output Ratio GOR calculation 3 Adding a new Thermal Vapor Compression TVC option The RO model upgrade includes 1 New and validated correlations for feed pressure and permeate salinity accounting for the effects of feed salinity temperature and fouling 2 Anew correlation for recovery ratio estimates The coupling configuration upgrade includes a re categorization of the energy sources to follow current practice The coupling scheme selection follows turbine design steam vs gas and co generation features dual purpose vs heat only The energy source categorization includes nuclear fossil and renewable options with the latter being a new addition 4 DEEP 3 0 MODEL DESCRIPTION A flow chart for the overall programme layout is shown in Fig 5 Input Forms Sheets Performance Analysis Thermal RO Cost Anlaysis Thermal RO Output Sheets Fig 5 General DEEP program layout This section gives a brief overview of the models including the thermal and RO performance models as well as the costing model 4 1 Thermal performance model The flow chart for
12. emak emus m errem EO DEPO opp Planned outage rate a 8 0 110 Unplanned outage rate if O value is calculated Appo Operating availability Ler Lifetime of energy piant _____ _ Energy plant contingency factor sia a Tair Siespecifc inet air temp MEE aes Condenser to Interm loop approach DTca emp TurType urbine type ExtrCon BackPr DTft Interm loop temperature drop Difference between feed steam temp DT1s nd max brine temp DPip Intermediate loop pressure loss Intermediate loop pump efficiency Energy Plant Cost Data Ce Specific construction cost KW en eoe a INH et Fossil fuel annual real escalation ee eee 3 Specific fossil renewable fuel cost Cnsf Specific nuclear fuel cost MWh i i interestrate 4 Ye feurrencyreferenceyear ved initial construction date ___ Yi Jm ayearofoperation _____ twp ifetime of water plant y O LBKo ietmeofbackupneatsource 0 e Purhasdelecmotycost skw 00000 15 Distillation Plant Performance Data Input Variable Default RE Wc t Required capacity 100000 Seawater feed temp TDS Feed salinity hog pn A 0 Wduo Distillation plant modular unit size Tcmo Steam temperature oC if 0
13. erep 1500 ony vjep 1502 3502 S1ojoure1ed jueAo o1 1970 29 USISIG ewp Iamog 40f JADYIMO 7g 914 vjep doo ojerpeurioju Suidno ss uroiq pUIM Ie os o qeM9 uad serp eoo DD se8 5504 OPA SA o oAo Wes oo1nos euuoq Jo L ASIN OU GAW OW Teas Jo od T K uo 7 51500 pareys wy o1seA o1nsso1dxpoeq SA 2 eng 71 2449 8005 vjep 8005 SJOOYSYIOM orproods 010 ndur 1os erep uoneornuopt 9520 erep yooloid 1981 vjep 1291014 12 When starting a new case the user is presented with a Case Input form to allow data entry as shown in Fig 9 Specify Case and Configuration Data Project Beta Version Test Aug 15 2005 Case Hybrid Case CC MED RO Water Plant Capacity Feed Salinity 3500C ppm Feed Temperature 30 degC Total Capacity 100000 m3 d Distillation part 50 Interest Rate 5 96 Purchased Electricity Cost 0 06 kWh Power Plant Data Distillation Plant Data Reverse Osmosis Plant Data Thermal Power 1200 MWt Energy Recovery Fraction 30 96 Net Electric Power 600 MWe Maximum Brine Tempe
14. es GOR Temperature Range Distillate Flow Feed Flow Steam Flow Brine Flow Brine salinity Specific Heat Consumption RO Performance Description Recovery Ratio Permeate Flow Feed Flow Feed Pressure Product Quality Brine Flow Brine salinity Specific Power Consumption Cost results Specific Power Cost Description Fixed charge cost Fuel cost O amp M cost Decommissioning cost Levelized Electricity Cost 18 Specific Water Cost Description Fixed charge cost Heat cost Plant electricity cost Purchased electricity cost O amp M cost Project Power Plant Data Type Ref Thermal Power Ref Net Electric Power Construction Cost Fuel Cost Purchased Electricity Cost Interest Rate Configuration Switches Steam Source Intermediate Loop TVC Option Backup Heat RO Energy Recovery Device Un Te DEEP 3 0 SAMPLE CASES Summary of Performance and Cost Results 1 200 600 700 50 0 037 ExtrCon N A N N N A MW MW kW BOE kWh DEEP Version 3 0 Sep 2005 Water Plant Data Type Required capacity Hybrid Dist Capacity Dist Construction Cost Maximum Brine Temp Heating Steam Temp Dist Feed Temp Seawater Feed Salinity Hybrid RO Capacity RO Construction Cost RO Recovery Ratio RO Energy Recovery Efficiency RO Design Flux RO Feed Temp Case MED 100 000 N A 900 65 0 0 0 30 35000 0 N A N A N A N A N A N A CC MED
15. f Performance and Cost Results 1 200 600 700 50 0 037 ExtrCon N A N N PEX MW MW kW BOE kWh DEEP Version 3 0 Sep 2005 Water Plant Data Type Required capacity Hybrid Dist Capacity Dist Construction Cost Maximum Brine Temp Heating Steam Temp Dist Feed Temp Seawater Feed Salinity Hybrid RO Capacity RO Construction Cost RO Recovery Ratio RO Energy Recovery Efficiency RO Design Flux RO Feed Temp Case MED RO 100 000 50 000 900 65 0 0 0 30 35000 0 50 000 900 0 00 0 95 13 6 30 0 CC MED RO m d G C ppm m d 1 m hour C Lost Electricity Production Power to Heat Ratio Plant Thermal Utilization Distillation Performance of Effects Stages GOR Temperature Range Distillate Flow Feed Flow Steam Flow Brine Flow Brine salinity Specific Heat Consumption 10 0 259 62 8 9 8 0 20 50 000 100 000 72 20 50 000 70 000 80 67 MW MWe MWt 96 C kg s ppm kWh m RO Performance Recovery Ratio Permeate Flow Feed Flow Feed Pressure Product Quality Brine Flow Brine Saliniy Specific Power Consumption 0 42 50 000 120 000 56 1 279 70 000 60 000 2 91 bar ppm ppm kWh m Specific Power Costs Fixed charge cost Fuel cost O amp M cost Decommissioning cost Levelized Electricity Cost 0 008 0 075 0 006 N A
16. flows as well from stage to stage and cools itself by flashing a portion into steam which is re condensed on the outside of the tube bundles MSF plants need pre treatment of the seawater to avoid scaling by adding acid or advanced scale inhibiting chemicals If low cost materials are used for construction of the evaporators a separate deaerator is to be installed The vent gases from the deaeration together with any non condensable gases released during the flashing process are removed by steam jet ejectors and discharged to the atmosphere Flashing Stages Heating Steam Feed Seawater Brine Blow Down Brine Heater Fig 3 Sketch of MSF layout 2 2 Multiple effect distillation MED Figure 3 shows the schematic flow diagram of MED process using horizontal tube evapora tors In each effect heat is transferred from the condensing water vapour on one side of the tube bundles to the evaporating brine on the other side of the tubes This process is repeated successively in each of the effects at progressively lower pressure and temperature driven by the water vapour from the preceding effect In the last effect at the lowest pressure and tem perature the water vapour condenses in the heat rejection heat exchanger which is cooled by incoming seawater The condensed distillate is collected from each effect Some of the heat in the distillate may be recovered by flash evaporation to a lower pressure As a heat source low pressure s
17. m is also retained as a design parameter and as such can be input by the user or alternatively calculated given an input steam temperature Given as input the salt concentration factor CF the cooling seawater temperature gain and the product water flow rateW estimates for reject brine flow Wy make up feed flow Wr and condenser cooling water flow could also be calculated as follows Wy Wp 1 4 We 5 W 6 Where refers to the net condenser heat load and refers to the specific heat capacity of cooling water While specific heat transfer areas could also be calculated in DEEP in a straightforward man ner the current approach where user input is expected for specific capital costs m d is considered adequate for the purposes of DEEP and is therefore retained Lost Shaft Work Model In DEEP 3 0 the lost shaft work 15 calculated as follows except for the heat only case where it 15 set to zero as follows For the backpressure case Qis Qs 0 0 C With Qst Qer Where Qer refers to the condenser heat load N Tem T Tem 273 8 refers to low pressure turbine isentropic efficiency and and Tem refer to the condenser reference and modified temperatures in For the extraction case 9 With Qst Where hy is the steam latent heat assuming saturation conditions and is redefined as N
18. n by Wilf 7 which take into account feed temperature and salinity correction factors and have been verified against commercial design data Feed pressure Pr is calculated as follows Ps Api 14 Where Apa Qn Apn Cr Cs Cr 15 And Posm is the average osmotic pressure across the system Api is the corresponding pressure loss Apa and the design net driving pressure and flux Ap and are the nominal net driving pressure and flux and Ct Cs and c are correction factors related to temperature salinity and fouling Permeate salinity S on the other hand is calculated as follows Sp 1 Sr 95 Qa C t 16 Where Srrefers to feed salinity and c and c are correction factors related to recovery and temperature rg refers to the membrane salt reject fraction For the calculation of energy recovery Qe given the energy recovery efficiency er both Pelton type and work exchanger designs are modeled as follows For the Pelton design Qer 1 rm 17 Where refers to the available high pumping power adjusted for system losses 4 3 Hybrid performance model Hybrid methods refer to the use of a combined configuration usually an RO MED or an RO MSF configuration These configurations have been designed with an eye on improving product water quality and operational flexibility 8 and DEEP allows their simulation through a combination of
19. ns are automatically performed and the user could then look at the case results Upon closing the output sheet the user can then further edit the input and run a follow up case if desired The user has then the possibility of setting up a comparative presentation CP to compare main cost results from two or more cases as explained above An example of a CP comparison sheet view is shown in Fig 10 When quitting the program the user should make use of the exit button and in any case is cau tioned against saving the executable file DEEP3 xls which may cause problems All user data are designed to be stored in the case files and not in the executable file It is also adviasable to keep a backup copy of the executable file DEEP3 xls just in case the original 1s unintentionally corrupted 13 Water Cost CC 4MEDRO 15 CC MEDRO 15 CC MEDRO 30 CC4MEDRO 50 Nuclear Gas NGT4MEDRO 10 6 Tutine MEDRO 5 Fig 10 View of a comparative DEEP 3 0 presentation 6 DEEP 3 0 INPUT OUTPUT DESCRIPTION 6 1 Input sheet Case Identification amp Basic Configuration Input Variable Default Remarks ___ tot d _ f tet 0 energy pianttype o osiptype __ ____ 71 Reference couping diagram e 14 Energy Plant Performance Data Variable Her R
20. ocess the programme makes use of pre composed configuration templates subfolder templates DEEP also includes fea tures allowing a comparative result presentation of up to nine pre run cases and results are saved under the User Files CPs subfolder 5 1 Installing DEEP The installation of DEEP has been tested under Windows 2000 and Windows XP A mini mum free disk size of of 11 Mbytes is needed including about 3 MB for the executable file DEEP3 xls and 7 MB for the template folder The user should make sure that the DEEP3 folder is not write protected and that the Excel security level is not set to high in order to enable macros 5 2 Running a DEEP case The programme is executed by double clicking on the DEEP3 xls icon in the root folder At startup the user is prompted to enable macros and is presented with the main program win dow Options available to the user include the following options New case This option 15 selected to start a new case A Case Input Form is sented for input of the main case parameters View case This option is selected to load an existing case file 10 Edit input data This option is selected to edit input for an active case All data can be edited with the exception of the configuration options which can only be changed from the Case Input Form Double clicking on any cell marked in green allows the user to modify its content Show case results This option is
21. om previous versions including upgrades in thermal and membrane performance and costing models the coupling configuration matrix and the user interface Changes in the thermal performance model include a revision of the gain output ratio GOR calculation and its generalization to include thermal vapour compression effects Since energy costs continue to represent an important fraction of seawater desalination costs the lost shaft work model has been generalized to properly account for both backpressure and extraction systems For RO systems changes include improved modeling of system recovery feed pressure and permeate salinity taking into account temperature feed salinity and fouling correction factors The upgrade to the coupling technology configuration matrix includes a re categorization of the energy sources to follow turbine design steam vs gas and co generation features dual purpose vs heat only In addition cost data has also been updated to reflect current practice and the user interface has been refurbished and made user friendlier The IAEA officers responsible for this publication were M Methnani and B Misra of the Division of Nuclear Power EDITORIAL NOTE The use of particular designations of countries or territories does not imply any judgement by the publisher the IAEA as to the legal status of such countries or territories of their authorities and institutions or of the delimitation of their boundaries The men
22. rature 65 degC Recovery Ratio optional FuelCost so Steam Temperature optional degC Design Flux 13 6 1 02 Specific Construction Cost 700 kw Specific Construction Cost 900 m3 d Specific Construction Cost 900 3 4 First select a coupling configuration from the matrix of supported energy sources and desalination technologies Configuration Switches MED MSF RO MED RO MSF RO c 5 5 NUCLEAR STEAM TURBINE NSC MED NSC MSF NSC RO NSC MED RO NSC MSF RO Condensing NUCLEAR GAS TURBINE NBC MSF NBC RO NBC MED RO NBC MSF RO C Backpressure NUCLEAR HEAT NH MED NH MSF STEAM CYCLE COAL COAL MED COAL MSF COAL RO COAL MED RO COAL MSF RO FOSSIL HEAT Backup heat source RENEWABLE HEAT RH MED RH MSF MED RO STAND ALONE RO SA RO New CC MED RO OK Fig 9 View of case input form The user is expected to first select the desired coupling configuration from the matrix of sup ported energy and desalination coupling options and also specify the name of the case save file Default values for the main parameters are then presented to the user who can edit them as ap proprate for the case Because error checking in DEEP is minimal the user is cautioned to check the accuracy of the input data entered Upon selecting the OK button spreadsheet calculatio
23. s Singapore 2005 OLIVER D Changing perspectives on desalination with renewable energy Interna tional Desalination Association Congress Singapore 2005 INTERNATIONAL ATOMIC ENERGY AGENCY Methodology for the Economic Evaluation of Cogeneration Desalination Options A User s Manual Computer Manual Series No 12 IAEA Vienna 1997 INTERNATIONAL ATOMIC ENERGY AGENCY Desalination Economic Evaluation Program DEEP User s Manual Computer Manual Series No 14 IAEA Vienna 2000 METHNANI M Recent model developments for the Desalination Economic Evalua tion Program DEEP International Desalination Association Congress Singapore 2005 BUROS O K The ABC of Desalting International Desalination Association Publi cation 1990 WILF M Review and modifications in the correlations of the RO part of the Agency s software DEEP Consultancy Report IAEA 2004 MOSER Design and operation of the largest hybrid desalination plant Fujairah International Desalination Association IDA Congress Singapore 2005 INTERNATIONAL ATOMIC ENERGY AGENCY Costing Methods for Nuclear De salination Technical Reports Series No 69 IAEA Vienna 1966 23 Louis P Methnani M Misra B Wilf M Wagner K CONTRIBUTORS TO DRAFTING AND REVIEW International Atomic Energy Agency International Atomic Energy Agency International Atomic Energy Agency Consultant United States of America Consultant C
24. s a portion of the water passes through the membrane the salt content in the remaining brine increases At the same time a portion of this brine is discharged without passing through the membrane RO membranes are made in a variety of modular configurations Two of the commercially successful configurations are spiral wound modules and hollow fibre modules The mem brane performance of RO modules such as salt rejection permeate product flow and mem brane compaction resistance were improved tremendously in the last years The DEEP per formance models cover both the effect of seawater salinity and the effect of seawater tempera ture on recovery ratio and required feedwater pressure A key criterion for the RO layout is the specific electricity consumption which should be as low as possible That means the recovery ratio has to be kept as high as possible and the ac companying feedwater pressure as low as possible fulfilling the drinking water standards as well as the design guidelines of the manufactures Since the overall recovery ratios of current seawater RO plants are only 30 to 50 and since the pressure of the discharge brine is only slightly less than the feed stream pressure all large scale seawater RO plants as well as many smaller plants are equipped with energy recovery turbines 3 DEEP 3 0 PROGRAM CHANGES Version three features important changes from previous versions including upgrades in thermal and membrane performance and
25. selected to show results for an active case The output summary includes main case parameters and configuration options as well as performance and cost results It can be printed on a single sheet New edit CP This option is selected to start a new Comparative Presentation CP case for side to side comparison of existing cases The user may be prompted to update reference links to the CPnull template located in the DEEP 3 0 root directory and is then prompted to specify the name of the CP save file and to select the cases to be compared View CP This option is selected to load an existing CP presentation file Show CP results This option is selected to show contents of an active CP presentation View directories This option is selected to view the DEEP 3 0 directory structure 5 3 Case input form The flowchart for input data is shown in Fig 8 81500 2 erep SOO pareys BYCP 1500 POLJA 2 aue d 15 uoneznioury vjep 3502 dnyoeg ewp 2502 WYO vjep 3502 150 481909 104 OAL 10 one JodeA 598215 5120 1 9 Jo 1equinN do 10 WEIJS soseo Jewry 104 jtur es poo 19 M vjep yeoy e qe reA 10 jroedeo USISIG ep jue d AA vjep 1500 VO 52
26. this model is shown in Fig 6 GOR Calculation Flow Pumping Power Calculations Lost Shaft Work Fig 6 Flowchart for thermal performance model GOR Model In the DEEP 3 0 model the user has the choice of specifying the GOR as a design parameter or letting the program calculate an estimate For MSF systems the GOR is calculated as follows An cn dTpn 1 dT ao 1 And for MED systems the GOR is calculated as follows An Am dTao dT pn dT ppe 2 Where latent heat of heating vapour kJ kg average latent heat of water vapour in MSF stages kJ kg maximum brine temperature C seawater temperature DTas brine to seawater temperature difference in last stage C Ch specific heat capacity of feedwater in brine heater kJ kg K Cm average specific heat capacity of brine in MSF plant kJ kg K overall working temperature range C average temperature drop per effect C brine heater feed temperature gain for MSF C boiling point elevation C dT ph Preheating feed temperature gain C For the case of thermal vapor compression units coupled to MED or MSF systems the GOR model is generalized as follows 1 3 Where Ry is defined as the ratio of entrained vapour flow to motive steam flow an input de sign parameter The top brine temperature T
27. tion of names of specific companies or products whether or not indicated as registered does not imply any intention to infringe proprietary rights nor should it be construed as an endorsement or recommendation on the part of the IAEA CONTENTS INTRODUCTION oet ehe es ale idee doi wind inate bue 1 2 DESALINATION PROCESSES on en 1 2 1 Multi stage flash MSF distillation nnne 2 2 2 Multiple effect distillation 3 2 3 MED plants with vapour compression eene 4 2 4 18 ise da deu teet ede ta iege 4 3 2 DEEP 3 0 PROGRAM CHANGES 4 4 ar vedete ah Evite 5 4 1 Thermal performance 4 1 sss eere enne nre 6 4 2 RO performance B o RE Rear etd d bedienen 8 4 3 Hybrid performance mod les ia eerte pr i e pe PSU ce 9 44 Costmodelz x een 9 5 DEEP 3 0 PROGRAM INSTRUCTIONS ica Msn 10 5 1 Installing DEEP unt tete e etta sete tatis 10 5 2 R nning DEEP c se tede t ra HO RETE EO 10 5 3 Case Input in prie tr n c tee etre e eee ee EH NR 11
28. value is calculated TVC Thermal vapor compression option Rwo Vovapremanmentrto Jo __ Esd Seawater pump efficiency 0 85 _____ 5 ____ 8 kWem __ y OE phmedowgerte od ____ O BK pacuphetsomeopionfeg SSS opb Backup heat planned outage rate ub cub Backup heatunplannedoutagerate Distillation Plant Cost Data Input Variable Description Unit Default Remarks Reference modular unit size for cost kdi Specific O amp M chemicals cost for pre reatment Specific O amp M chemicals cost for post cdcpo reatment ____ _____ O amp M insurance cost heat source unit cost MW t 39000 Fossil fuel price for backup heat source 20 Cffb at startup bbl Fossil fuel real escala for backup heat 2 effb ource la ___ of management personnel ts calculated HI Cet of labor personnel 16 RO Plant Performance Data Wct Required capacity __Tamo_fROfecawaterinettemperatre e 0 00 Wmo DPsm ____ Seawater pump efficiency EU EE ERR Ro Dflux Design flux l m2 h eer Emegyreoveyeficieny _ EerType RO energy recovery devicetype Jo TIPPER DPbm Booserpumphead J a ooo
29. w version DEEP 3 0 has been released 5 The program allows designers and decision makers to compare performance and cost estimates of various desalination and power configurations Desalination options modeled include MSF MED RO and hybrid systems while power options include nuclear fossil and renewable sources Both co generation of electricity and water as well as water only plants can be modeled The program also enables a side by side comparison of a number of design alternatives which helps identify the lowest cost options for water and power production at a specific location Data needed include the desired configuration power and water capacities as well as values for the various basic performance and costing data 2 DESALINATION PROCESSES Desalination systems fall into two main design categories namely thermal and membrane types 6 Thermal designs including multi stage flash MSF and Multi effect distillation MED use flashing and evaporation to produce potable water while membrane designs use the method of Reverse Osmosis RO shown in Fig 1 With continuing improvements in membrane performance RO technology is increasingly gaining markets in seawater desalination and hybrid configurations combining RO with MED or RO with MSF have also been considered Fig 2 Membrane Module Feed Seawater Distillate Feed Treatment Energy Recovery Product Treatment Brine Reject Fig 1 Sketch of RO layout
30. y Efficiency RO Design Flux RO Feed Temp Case RO 100 000 N A N A N A N A N A 35000 0 N A 900 0 00 0 95 13 6 30 0 Stand Alone RO m d C C C ppm 1 m hour Lost Electricity Production Power to Heat Ratio Plant Thermal Utilization Distillation Performance of Effects Stages GOR Temperature Range Distillate Flow Feed Flow Steam Flow Brine Flow Brine salinity Specific Heat Consumption N A N A N A N A N A N A N A N A N A N A N A N A MW MWe MWt C kg s ppm kWh m RO Performance Recovery Ratio Permeate Flow Feed Flow Feed Pressure Product Quality Brine Flow Brine Saliniy Specific Power Consumption 0 42 105 000 252 000 56 1 279 147 000 60 000 2 97 ppm ppm kWh m Specific Power Costs Fixed charge cost Fuel cost O amp M cost Decommissioning cost Levelized Electricity Cost N A N A N A N A N A kWh kWh kWh kWh kWh Specific Water Costs Fixed charge cost Heat cost Plant electricity cost Purchased electricity cost O amp M cost Total Specific Water Cost 0 278 N A 0 000 0 110 0 173 0 562 m m m m m m 1 2 3 4 5 6 7 8 9 REFERENCES MISRA B Status and prospects of nuclear desalination International Desalination Association Congres
31. zech Republic 25 E id O Ll a ILL Fr HE EI pp n SST 9 seers DI INTERNATIONAL ATOMIC ENERGY AGENCY VIENNA
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