Changeset 354 for trunk/eml


Ignore:
Timestamp:
Aug 30, 2007, 2:17:16 PM (15 years ago)
Author:
Argimiro Resende Secchi
Message:

Fixing more wiki notation.

Location:
trunk/eml
Files:
19 edited

Legend:

Unmodified
Added
Removed

  • trunk/eml/controllers/Comparator.mso

    r306 r354  
    2626        Brief           = "Model Comparator.";
    2727        Info            =
    28         "
    29         - Inputs:
    30         * Two different input signals.
     28"== Inputs ==
     29* Two different input signals.
    3130       
    32         - Outputs:
    33         * One output signal.
    34         ";
     31== Outputs ==
     32* One output signal.
     33";
    3534       
    3635        VARIABLES

  • trunk/eml/controllers/HiLoSelect.mso

    r306 r354  
    2626        Brief           = "Model HiLo Select.";
    2727        Info            =
    28         "
    29         - Inputs:
    30         * Two different input signals.
     28"== Inputs ==
     29* Two different input signals.
    3130       
    32         - Outputs:
    33         * One output signal.
    34        
    35         ";
     31== Outputs ==
     32* One output signal.
     33";
    3634       
    3735        PARAMETERS

  • trunk/eml/controllers/PIDIncr.mso

    r306 r354  
    9696        Brief           = "Model of incremental PIDs.";
    9797        Info            =
    98         "
    99         - Inputs
    100         *       - a scaled processs variable.
    101         *       - a scaled bias.
    102         *       - a scaled setpoint.
    103 
    104         - Outputs
    105         *  - a scaled output.
    106         ";
     98"== Inputs ==
     99* scaled processs variable.
     100* scaled bias.
     101* scaled setpoint.
     102
     103== Outputs ==
     104* a scaled output.
     105";
    107106       
    108107        PARAMETERS

  • trunk/eml/controllers/PIDs.mso

    r306 r354  
    9595        Brief           = "Model of PIDs.";
    9696        Info            =
    97         "
    98         - Inputs
    99         *       - a scaled processs variable.
    100         *       - a scaled bias.
    101         *       - a scaled setpoint.
    102 
    103         - Outputs
    104         *  - a scaled output.
    105         ";
     97"== Inputs ==
     98* scaled processs variable.
     99* scaled bias.
     100* scaled setpoint.
     101
     102== Outputs ==
     103* scaled output.
     104";
    106105       
    107106        PARAMETERS

  • trunk/eml/controllers/iae.mso

    r306 r354  
    2727        Brief           = "Model IAE.";
    2828        Info            =
    29         "
    30         - Inputs:
    31         * One input signal.
    32         * One setpoint signal.
     29"== Inputs ==
     30* One input signal.
     31* One setpoint signal.
    3332       
    34         - Outputs:
    35         * One output signal.
    36         ";
     33== Outputs ==
     34* One output signal.
     35";
    3736       
    3837        VARIABLES

  • trunk/eml/controllers/ise.mso

    r306 r354  
    2727        Brief           = "Model ISE.";
    2828        Info            =
    29         "
    30         - Inputs:
    31         * One input signal.
    32         * One setpoint signal.
     29"== Inputs ==
     30* One input signal.
     31* One setpoint signal.
    3332       
    34         - Outputs:
    35         * One output signal.
    36         ";
     33== Outputs ==
     34* One output signal.
     35";
    3736       
    3837        VARIABLES

  • trunk/eml/controllers/lag_1.mso

    r306 r354  
    2727        Brief           = "Model Lag.";
    2828        Info            =
    29         "
    30         - Inputs:
    31         * One input signal.
     29"== Inputs ==
     30* One input signal.
    3231       
    33         - Outputs:
    34         * One output signal.
    35         ";
     32== Outputs ==
     33* One output signal.
     34";
    3635       
    3736        PARAMETERS

  • trunk/eml/controllers/lead_lag.mso

    r306 r354  
    2727        Brief           = "Model Lead lag.";
    2828        Info            =
    29         "
    30         - Inputs:
    31         * One input signal.
     29"== Inputs ==
     30* One input signal.
    3231       
    33         - Outputs:
    34         * One output signal.
    35         ";
     32== Outputs ==
     33* One output signal.
     34";
    3635       
    3736        PARAMETERS

  • trunk/eml/controllers/multiply.mso

    r306 r354  
    2727        Brief           = "Model Multiply.";
    2828        Info            =
    29         "
    30         - Inputs:
    31         * Two input signals.
     29"== Inputs ==
     30* Two input signals.
    3231       
    33         - Outputs:
    34         * One output signal.
    35        
    36         ";
     32== Outputs ==
     33* One output signal.
     34";
    3735       
    3836        VARIABLES

  • trunk/eml/controllers/ratio.mso

    r306 r354  
    2626        Brief           = "Model Ratio.";
    2727        Info            =
    28         "
    29         - Inputs:
    30         * Two input signals.
     28"== Inputs ==
     29* Two input signals.
    3130       
    32         - Outputs:
    33         * One output signal.
    34         ";
     31== Outputs ==
     32* One output signal.
     33";
    3534       
    3635        VARIABLES

  • trunk/eml/controllers/sum.mso

    r306 r354  
    2626        Brief           = "Model Sum.";
    2727        Info            =
    28         "
    29         - Inputs:
    30         * Two input signals.
     28"== Inputs ==
     29* Two input signals.
    3130       
    32         - Outputs:
    33         * One output signal.
    34         ";
     31== Outputs ==
     32* One output signal.
     33";
    3534       
    3635        VARIABLES

  • trunk/eml/costs/column_cost.mso

    r331 r354  
    4141        Brief           = "Model of a distillation column with dynamic condenser and dynamic reboiler.";
    4242        Info            =
    43         "Specify:
    44          * the feed stream of each tray (Inlet);
    45          * the Murphree eficiency for each tray Emv;
    46          * the pump pressure difference;
    47          * the heat supllied in reboiler and condenser;
    48          * the condenser vapor outlet flow (OutletV.F);
    49          * the reboiler liquid outlet flow (OutletL.F);
    50          * both splitter outlet flows OR one of the splitter outlet flows and the splitter frac.
    51          * all necessary dimensions and materials for cost evaluation
    52        
    53         Initial Conditions:
    54          * the trays temperature (OutletL.T);
    55          * the trays liquid level (Level) OR the trays liquid flow (OutletL.F);
    56          * (NoComps - 1) OutletL (OR OutletV) compositions for each tray;
    57        
    58          * the condenser temperature (OutletL.T);
    59          * the condenser liquid level (Level);
    60          * (NoComps - 1) OutletL (OR OutletV) compositions;
    61        
    62          * the reboiler temperature (OutletL.T);
    63          * the reboiler liquid level (Level);
    64          * (NoComps - 1) OutletL (OR OutletV) compositions.
    65         ";
     43"== Specify ==
     44* the feed stream of each tray (Inlet);
     45* the Murphree eficiency for each tray Emv;
     46* the pump pressure difference;
     47* the heat supllied in reboiler and condenser;
     48* the condenser vapor outlet flow (OutletV.F);
     49* the reboiler liquid outlet flow (OutletL.F);
     50* both splitter outlet flows OR one of the splitter outlet flows and the splitter frac.
     51* all necessary dimensions and materials for cost evaluation
     52       
     53== Initial Conditions ==
     54* the trays temperature (OutletL.T);
     55* the trays liquid level (Level) OR the trays liquid flow (OutletL.F);
     56* (NoComps - 1) OutletL (OR OutletV) compositions for each tray;
     57       
     58* the condenser temperature (OutletL.T);
     59* the condenser liquid level (Level);
     60* (NoComps - 1) OutletL (OR OutletV) compositions;
     61       
     62* the reboiler temperature (OutletL.T);
     63* the reboiler liquid level (Level);
     64* (NoComps - 1) OutletL (OR OutletV) compositions.
     65";
    6666
    6767        PARAMETERS
    … …  
    163163        Brief           = "Model of a distillation column with steady condenser and steady reboiler.";
    164164        Info            =
    165         "Specify:
    166          * the feed stream of each tray (Inlet);
    167          * the Murphree eficiency for each tray Emv;
    168          * the pump head;
    169          * the condenser pressure drop;
    170          * the heat supllied in top and bottom tanks;
    171          * the heat supllied in condenser and reboiler;
    172          * the Outlet1 flow in the bottom splitter (spbottom.Outlet1.F) that corresponds to the bottom product;
    173          * both  top splitter outlet flows OR one of the splitter outlet flows and the splitter frac.
    174          * all necessary dimensions and materials for cost evaluation
    175 
    176         Initial Conditions:
    177          * the trays temperature (OutletL.T);
    178          * the trays liquid level (Level) OR the trays liquid flow (OutletL.F);
    179          * (NoComps - 1) OutletL (OR OutletV) compositions for each tray;
    180        
    181          * the top tank temperature (OutletL.T);
    182          * the top tank liquid level (Level);
    183          * (NoComps - 1) OutletL (OR OutletV) compositions;
    184        
    185          * the bottom tank temperature (OutletL.T);
    186          * the bottom tank liquid level (Level);
    187          * (NoComps - 1) OutletL (OR OutletV) compositions.
    188         ";
     165"== Specify ==
     166* the feed stream of each tray (Inlet);
     167* the Murphree eficiency for each tray Emv;
     168* the pump head;
     169* the condenser pressure drop;
     170* the heat supllied in top and bottom tanks;
     171* the heat supllied in condenser and reboiler;
     172* the Outlet1 flow in the bottom splitter (spbottom.Outlet1.F) that corresponds to the bottom product;
     173* both  top splitter outlet flows OR one of the splitter outlet flows and the splitter frac.
     174* all necessary dimensions and materials for cost evaluation
     175
     176== Initial Conditions ==
     177* the trays temperature (OutletL.T);
     178* the trays liquid level (Level) OR the trays liquid flow (OutletL.F);
     179* (NoComps - 1) OutletL (OR OutletV) compositions for each tray;
     180       
     181* the top tank temperature (OutletL.T);
     182* the top tank liquid level (Level);
     183* (NoComps - 1) OutletL (OR OutletV) compositions;
     184       
     185* the bottom tank temperature (OutletL.T);
     186* the bottom tank liquid level (Level);
     187* (NoComps - 1) OutletL (OR OutletV) compositions.
     188";
    189189
    190190        PARAMETERS
    … …  
    286286        Brief           = "Model of a distillation column with dynamic condenser and steady reboiler.";
    287287        Info            =
    288         "Specify:
    289          * the feed stream of each tray (Inlet);
    290          * the Murphree eficiency for each tray Emv;
    291          * the pump head;
    292          * the condenser vapor outlet flow (OutletV.F);
    293          * the heat supllied in bottom tank;
    294          * the heat supllied in condenser and reboiler;
    295          * the Outlet1 flow in the bottom splitter (spbottom.Outlet1.F) that corresponds to the bottom product;
    296          * all necessary dimensions and materials for cost evaluation
    297 
    298         Initial Conditions:
    299          * the trays temperature (OutletL.T);
    300          * the trays liquid level (Level) OR the trays liquid flow (OutletL.F);
    301          * (NoComps - 1) OutletL (OR OutletV) compositions for each tray;
    302        
    303          * the condenser temperature (OutletL.T);
    304          * the condenser liquid level (Level);
    305          * (NoComps - 1) OutletL (OR OutletV) compositions;
    306        
    307          * the bottom tank temperature (OutletL.T);
    308          * the bottom tank liquid level (Level);
    309          * (NoComps - 1) OutletL (OR OutletV) compositions.
    310         ";
     288"== Specify ==
     289* the feed stream of each tray (Inlet);
     290* the Murphree eficiency for each tray Emv;
     291* the pump head;
     292* the condenser vapor outlet flow (OutletV.F);
     293* the heat supllied in bottom tank;
     294* the heat supllied in condenser and reboiler;
     295* the Outlet1 flow in the bottom splitter (spbottom.Outlet1.F) that corresponds to the bottom product;
     296* all necessary dimensions and materials for cost evaluation
     297
     298== Initial Conditions ==
     299* the trays temperature (OutletL.T);
     300* the trays liquid level (Level) OR the trays liquid flow (OutletL.F);
     301* (NoComps - 1) OutletL (OR OutletV) compositions for each tray;
     302       
     303* the condenser temperature (OutletL.T);
     304* the condenser liquid level (Level);
     305* (NoComps - 1) OutletL (OR OutletV) compositions;
     306       
     307* the bottom tank temperature (OutletL.T);
     308* the bottom tank liquid level (Level);
     309* (NoComps - 1) OutletL (OR OutletV) compositions.
     310";
    311311
    312312        PARAMETERS
    … …  
    406406        Brief           = "Model of a distillation column with steady condenser and dynamic reboiler.";
    407407        Info            =
    408         "Specify:
    409          * the feed stream of each tray (Inlet);
    410          * the Murphree eficiency for each tray (Emv);
    411          * the pump pressure difference;
    412          * the heat supllied in reboiler and condenser;
    413          * the heat supllied in the top tank;
    414          * the condenser pressure drop;
    415          * the reboiler liquid outlet flow (OutletL.F);
    416          * both splitter outlet flows OR one of the splitter outlet flows and the splitter frac.
    417          * all necessary dimensions and materials for cost evaluation
    418 
    419         Initial Conditions:
    420          * the trays temperature (OutletL.T);
    421          * the trays liquid level (Level) OR the trays liquid flow (OutletL.F);
    422          * (NoComps - 1) OutletL (OR OutletV) compositions for each tray;
    423        
    424          * the top tank temperature (OutletL.T);
    425          * the top tank liquid level (Level);
    426          * (NoComps - 1) OutletL (OR OutletV) compositions;
    427        
    428          * the reboiler temperature (OutletL.T);
    429          * the reboiler liquid level (Level);
    430          * (NoComps - 1) OutletL (OR OutletV) compositions.
    431         ";
     408"== Specify ==
     409* the feed stream of each tray (Inlet);
     410* the Murphree eficiency for each tray (Emv);
     411* the pump pressure difference;
     412* the heat supllied in reboiler and condenser;
     413* the heat supllied in the top tank;
     414* the condenser pressure drop;
     415* the reboiler liquid outlet flow (OutletL.F);
     416* both splitter outlet flows OR one of the splitter outlet flows and the splitter frac.
     417* all necessary dimensions and materials for cost evaluation
     418
     419== Initial Conditions ==
     420* the trays temperature (OutletL.T);
     421* the trays liquid level (Level) OR the trays liquid flow (OutletL.F);
     422* (NoComps - 1) OutletL (OR OutletV) compositions for each tray;
     423       
     424* the top tank temperature (OutletL.T);
     425* the top tank liquid level (Level);
     426* (NoComps - 1) OutletL (OR OutletV) compositions;
     427       
     428* the reboiler temperature (OutletL.T);
     429* the reboiler liquid level (Level);
     430* (NoComps - 1) OutletL (OR OutletV) compositions.
     431";
    432432
    433433        PARAMETERS

  • trunk/eml/heat_exchangers/PHE.mso

    r352 r354  
    2525        Brief           = "Shortcut model  for plate and Frame heat exchanger.";
    2626        Info            =
    27         "
    28         Model of a gasketed plate heat exchanger.
    29         The heat transfer and pressure loss calculations are based on Kumar [1] work.
    30         The following assumptions are considered in order to derive the mathematical model [2]:
    31        
    32         A.1 : Steady-State operation;
    33         A.2 : No phase changes;
    34         A.3 : No heat loss to the surroundings.
    35         A.4 : Uniform distribution of flow through the channels of a pass.
    36 
    37         References:
     27"Model of a gasketed plate heat exchanger.
     28The heat transfer and pressure loss calculations are based on Kumar [1] work.
     29The following assumptions are considered in order to derive the mathematical model [2]:
     30
     31== Assumptions ==
     32* Steady-State operation;
     33* No phase changes;
     34* No heat loss to the surroundings.
     35* Uniform distribution of flow through the channels of a pass.
     36
     37== References ==
    3838   
    39         [1] E.A.D. Saunders, Heat Exchangers: Selection, Design and
    40     Construction, Longman, Harlow, 1988.
     39[1] E.A.D. Saunders, Heat Exchangers: Selection, Design and
     40Construction, Longman, Harlow, 1988.
    4141   
    42         [2] J.A.W. Gut, J.M. Pinto, Modeling of plate heat exchangers
    43     with generalized configurations, Int. J. Heat Mass Transfer
    44     46 (14) (2003) 2571\2585.
    45         ";
     42[2] J.A.W. Gut, J.M. Pinto, Modeling of plate heat exchangers
     43with generalized configurations, Int. J. Heat Mass Transfer
     4446 (14) (2003) 2571\2585.
     45";
    4646
    4747 PARAMETERS

  • trunk/eml/mixers_splitters/mixer.mso

    r351 r354  
    2525        Icon            = "icon/mixer";
    2626        Brief           = "Model of a mixer";
    27         Info            = "
    28         Assumptions:
    29          * thermodynamics equilibrium
    30          * adiabatic
     27        Info            =
     28"== Assumptions ==
     29* thermodynamics equilibrium
     30* adiabatic
    3131       
    32         Specify:
    33          * the inlet streams";
     32== Specify ==
     33* the inlet streams";
    3434       
    3535        PARAMETERS

  • trunk/eml/mixers_splitters/sepComp.mso

    r351 r354  
    2525        Icon            = "icon/splitter_n";
    2626        Brief           = "Model of a separator of components";
    27         Info            = "
    28         Assumptions:
    29          * thermodynamics equilibrium
    30          * adiabatic
    31        
    32         Specify:
    33                 * the inlet stream
    34                 * (NComp - 1) molar fractions to (Noutlet - 1) outlet streams
    35                 * (Noutlet - 1) frac (fraction of split of the outlet streams):
    36                                
    37                                         frac(i) = (Mole Flow of the outlet stream i /
    38                                                                         Mole Flow of the inlet stream)
    39                                                                                                         where i = 1, 2,...,Noutlet
     27        Info            =
     28"== Assumptions ==
     29* thermodynamics equilibrium
     30* adiabatic
     31
     32== Specify ==
     33* the inlet stream
     34* (NComp - 1) molar fractions to (Noutlet - 1) outlet streams
     35* (Noutlet - 1) frac (fraction of split of the outlet streams):
     36                       
     37        frac(i) = (Mole Flow of the outlet stream i /
     38                                Mole Flow of the inlet stream)
     39                                                where i = 1, 2,...,Noutlet
    4040                        or
    4141
    42                   (Noutlet - 1) recovery (Recovery of the component specified in the outlet stream i):
     42  (Noutlet - 1) recovery (Recovery of the component specified in the outlet stream i):
    4343
    44                                         recovery(i) = (Mole Flow of the component specified in the Outlet stream i/
    45                                                                                 Mole Flow of the component specified in the inlet stream)
    46                                                                                                         where i = 1, 2,...,Noutlet
    47         ";
     44  recovery(i) = (Mole Flow of the component specified in the Outlet stream i/
     45                                Mole Flow of the component specified in the inlet stream)
     46                                                where i = 1, 2,...,Noutlet
     47";
    4848       
    4949PARAMETERS
    … …  
    115115        Icon            = "icon/splitter";
    116116        Brief           = "Model of a separator of components";
    117         Info            = "
    118         Assumptions:
    119          * thermodynamics equilibrium
    120          * adiabatic
     117        Info            =
     118"== Assumptions ==
     119* thermodynamics equilibrium
     120* adiabatic
    121121       
    122         Specify:
    123                 * the inlet stream
    124                 * (NComp - 1) molar fractions to 1 of the outlet streams
    125                 * the fraction of split of the outlet streams
    126         ";
     122== Specify ==
     123* the inlet stream
     124* (NComp - 1) molar fractions to 1 of the outlet streams
     125* the fraction of split of the outlet streams
     126";
    127127
    128128PARAMETERS

  • trunk/eml/mixers_splitters/splitter.mso

    r351 r354  
    2626        Icon            = "icon/splitter_n";
    2727        Brief           = "Model of a splitter";
    28         Info            = "
    29         Assumptions:
    30                 * thermodynamics equilibrium
    31                 * adiabatic
     28        Info            =
     29"== Assumptions ==
     30* thermodynamics equilibrium
     31* adiabatic
    3232                       
    33         Specify:
    34                 * the inlet stream
    35                 * (Noutlet - 1) fraction of split of the outlet streams:
    36                                 frac(i) = (Mole Flow of the outlet stream i /
    37                                                                         Mole Flow of the inlet stream)
     33== Specify ==
     34* the inlet stream
     35* (Noutlet - 1) fraction of split of the outlet streams:
     36
     37        frac(i) = (Mole Flow of the outlet stream i /
     38                                Mole Flow of the inlet stream)
    3839                                where i = 1, 2,...,Noutlet
    39         ";
     40";
    4041       
    4142        PARAMETERS
    … …  
    8081        Icon            = "icon/splitter";
    8182        Brief           = "Splitter with 2 outlet streams";
    82         Info            = "
    83         Assumptions:
    84                 * thermodynamics equilibrium
    85                 * adiabatic
     83        Info            =
     84"== Assumptions ==
     85* thermodynamics equilibrium
     86* adiabatic
    8687                       
    87         Specify:
    88                 * the inlet stream
    89                 * (Noutlet - 1) fraction of split of the outlet streams:
    90                                 frac(i) = (Mole Flow of the outlet stream i /
    91                                                                         Mole Flow of the inlet stream)
     88== Specify ==
     89* the inlet stream
     90* (Noutlet - 1) fraction of split of the outlet streams:
     91
     92        frac(i) = (Mole Flow of the outlet stream i /
     93                                Mole Flow of the inlet stream)
    9294                                where i = 1, 2,...,Noutlet
    93         ";
     95";
    9496
    9597        VARIABLES

  • trunk/eml/reactors/batch.mso

    r352 r354  
    2525        Icon            = "icon/batch";
    2626        Brief           = "Model of a batch reactor";
    27         Info            = "
    28         Assumptions
    29          * isothermic
    30         ";
     27        Info            =
     28"== Assumptions ==
     29* isothermic
     30";
    3131
    3232PARAMETERS

  • trunk/eml/reactors/pfr.mso

    r352 r354  
    2626        Brief           = "Model of a Generic PFR with constant mass holdup";
    2727        Icon            = "icon/pfr";
    28         Info            = "
    29         Requires the information of:
    30          * Reaction values
    31          * Heat of reaction
    32          * Pressure profile
    33         ";
     28        Info            =
     29"== Requires the information of ==
     30* Reaction values
     31* Heat of reaction
     32* Pressure profile
     33";
    3434
    3535PARAMETERS

  • trunk/eml/water_steam/power_plant.mso

    r315 r354  
    5555        VARIABLES
    5656        H_IS            as Entalpia;
    57         EF_T            as Eficiencia(Brief="Eficiencia da turbina");
    58         POT_TURB        as Potencia(Brief="Potencia da turbina");
    59 in      Fin             as Corrente;
    60 out     Fout    as Corrente;
     57        EF_T            as Eficiencia (Brief="Eficiencia da turbina");
     58        POT_TURB        as Potencia (Brief="Potencia da turbina");
     59in      Fin             as Corrente (Symbol="_{in}");
     60out     Fout    as Corrente (Symbol="_{out}");
    6161
    6262        EQUATIONS
    … …  
    8383        POT_TURB        as Potencia(Brief="Potencia da turbina");
    8484        y                       as Fracao(Brief="Fracao massica da sangria");
    85 in      Fin                     as Corrente;
    86 out Fout                as Corrente;
    87 out Fouts               as Corrente;#(Brief="Sangria da Turbina")
     85in      Fin                     as Corrente (Symbol="_{in}");
     86out Fout                as Corrente (Symbol="_{out}");
     87out Fouts               as Corrente (Symbol="_{outx}");#(Brief="Sangria da Turbina")
    8888
    8989        EQUATIONS
    … …  
    111111       
    112112        VARIABLES
    113         Q_COND  as Potencia(Brief="Taxa de calor removido");
    114         G_S             as Dif_Temp(Brief="Grau de sub-resfriamento");
    115 in      Fin             as Corrente;
    116 out     Fout    as Corrente;
     113        Q_COND  as Potencia (Brief="Taxa de calor removido");
     114        G_S             as Dif_Temp (Brief="Grau de sub-resfriamento");
     115in      Fin             as Corrente (Symbol="_{in}");
     116out     Fout    as Corrente (Symbol="_{out}");
    117117
    118118        EQUATIONS
    … …  
    133133   
    134134        VARIABLES
    135         Q_COND  as Potencia(Brief="Taxa de calor removido");
    136         G_S             as Dif_Temp(Brief="Grau de sub-resfriamento");
    137 in      Fin1    as Corrente(Brief="Corrente com pressao igual a saida");
    138 in      Fin2    as Corrente;
    139 out     Fout    as Corrente;
     135        Q_COND  as Potencia (Brief="Taxa de calor removido");
     136        G_S             as Dif_Temp (Brief="Grau de sub-resfriamento");
     137in      Fin1    as Corrente (Brief="Corrente com pressao igual a saida", Symbol="_{in1}");
     138in      Fin2    as Corrente (Symbol="_{in2}");
     139out     Fout    as Corrente (Symbol="_{out}");
    140140
    141141        EQUATIONS
    … …  
    156156       
    157157    VARIABLES
    158 in      Fin1    as Corrente;
    159 in      Fin2    as Corrente;
    160 in      Fin3    as Corrente;
    161 out     Fout    as Corrente;
     158in      Fin1    as Corrente (Symbol="_{in1}");
     159in      Fin2    as Corrente (Symbol="_{in2}");
     160in      Fin3    as Corrente (Symbol="_{in3}");
     161out     Fout    as Corrente (Symbol="_{out}");
    162162
    163163        EQUATIONS
    … …  
    177177        Q               as Potencia;
    178178        DP              as Dif_Pres;
    179 in      Fin             as Corrente;
    180 out     Fout    as Corrente;
     179in      Fin             as Corrente (Symbol="_{in}");
     180out     Fout    as Corrente (Symbol="_{out}");
    181181
    182182        EQUATIONS
    … …  
    226226        POT_EF  as Potencia(Brief="Potencia injetada pela bomba");
    227227        EF_B    as Eficiencia(Brief="Eficiencia da bomba");
    228 in      Fin             as Corrente;
    229 out     Fout    as Corrente;
     228in      Fin             as Corrente (Symbol="_{in}");
     229out     Fout    as Corrente (Symbol="_{out}");
    230230       
    231231        EQUATIONS
    … …  
    249249
    250250    VARIABLES
    251         Q_GV            as Potencia(Brief="Taxa de calor gerado na caldeira");
    252         EF_GV           as Eficiencia(Brief="Eficiencia do gerador de vapor");
    253         Qra                     as Potencia(Brief="Taxa de calor nos reaquecedores");
    254         Qsa                     as Potencia(Brief="Taxa de calor nos superaquecedores");
    255         Qca                     as Potencia(Brief="Taxa de calor no evaporador");
    256         Qec                     as Potencia(Brief="Taxa de calor nos economizadores");
    257 in      Fin_a           as Corrente(Brief="Agua de alimentacao");
    258 in      Fin_ra          as Corrente(Brief="Vapor a ser Reaquecido");
    259 out     Fout_sa     as Corrente(Brief="Vapor Superaquecido");
    260 out     Fout_ra     as Corrente(Brief="Vapor Reaquecido");
    261         Fvap            as Corrente(Brief="Evaporador");
    262         Feco            as Corrente(Brief="Economizadores");
     251        Q_GV            as Potencia (Brief="Taxa de calor gerado na caldeira");
     252        EF_GV           as Eficiencia (Brief="Eficiencia do gerador de vapor");
     253        Qra                     as Potencia (Brief="Taxa de calor nos reaquecedores");
     254        Qsa                     as Potencia (Brief="Taxa de calor nos superaquecedores");
     255        Qca                     as Potencia (Brief="Taxa de calor no evaporador");
     256        Qec                     as Potencia (Brief="Taxa de calor nos economizadores");
     257in      Fin_a           as Corrente (Brief="Agua de alimentacao", Symbol="_{in_a}");
     258in      Fin_ra          as Corrente (Brief="Vapor a ser Reaquecido", Symbol="_{in_ra}");
     259out     Fout_sa     as Corrente (Brief="Vapor Superaquecido", Symbol="_{out_sa}");
     260out     Fout_ra     as Corrente (Brief="Vapor Reaquecido", Symbol="_{out_ra}");
     261        Fvap            as Corrente (Brief="Evaporador");
     262        Feco            as Corrente (Brief="Economizadores");
    263263
    264264        EQUATIONS
    … …  
    298298        Q_GV            as Potencia;
    299299        EF_GV           as Eficiencia;
    300 in      Fin                     as Corrente;
    301 out     Fout            as Corrente;
     300in      Fin                     as Corrente (Symbol="_{in}");
     301out     Fout            as Corrente (Symbol="_{out}");
    302302
    303303        EQUATIONS
    … …  
    324324        VARIABLES
    325325        y                       as Fracao(Brief="Fracao de massa para a segunda corrente");
    326 in      Fin                     as Corrente;
    327 out     Fout            as Corrente;
    328 out     Fouts           as Corrente(Brief="Segunda corrente");
     326in      Fin                     as Corrente (Symbol="_{in}");
     327out     Fout            as Corrente (Symbol="_{out}");
     328out     Fouts           as Corrente(Brief="Segunda corrente", Symbol="_{outx}");
    329329
    330330        EQUATIONS
Note: See TracChangeset for help on using the changeset viewer.