source: branches/tests/eml/pressure_changers/pipe.mso @ 541

Last change on this file since 541 was 541, checked in by gerson bicca, 15 years ago

updated pipe model (testing)
File size: 16.6 KB
Line 
1
2using "streams";
3# Not Finished yet !!!!
4# Do Not Use it
5
6Model props
7
8ATTRIBUTES
9        Pallete         = false;
10        Brief           = "System properties for the pipe model";
11
12PARAMETERS
13
14outer   N               as Integer      (Brief = "Number of Profile Intervals", Default = 1, Lower = 1, Upper = 100);
15outer   NComp   as Integer      (Brief = "Number of chemical components", Lower = 1);
16       
17VARIABLES
18
19        Fw(N+1)                         as flow_mass    (Brief = "Mass Flow Profile" , Symbol = "F_w");
20        rho(N+1)                        as dens_mass    (Brief = "Mass Density Profile" , Symbol = "\rho");
21        mu(N+1)                         as viscosity            (Brief = "Viscosity Profile" , Symbol = "\mu");
22
23        Vel(N+1)                        as velocity     (Brief = "Velocity Profile");
24        vm(N+1)                         as vol_mol      (Brief = "Molar Volume Profile");
25        frac(N+1)                       as fraction     (Brief = "Molar Fraction Profile");
26        Vsfrac(N+1)                     as fraction     (Brief = "No Slip Volume Fraction Profile",Lower=0);
27        Holdup(N+1)                     as fraction     (Brief = "Holdup Profile",Lower=0);
28        Mfrac(N+1,NComp)        as fraction     (Brief = "Phase Molar Fraction Profile");
29        h(N+1)                          as enth_mol (Brief = "Molar Enthalpy profile");
30       
31end
32
33Model pipe
34
35ATTRIBUTES
36        Pallete         = true;
37        Icon            = "icon/pipe";         
38        Brief           = "pipe";
39        Info            =
40"This distributed model describes the pressure drop of a material stream flowing in a pipe.
41
42==Assumptions==
43*Cross sectional area is constant;
44*Newtonian fluid;
45*Steady-state;
46";
47
48PARAMETERS
49
50        outer   NComp   as Integer      (Brief = "Number of chemical components", Lower = 1);
51        outer  PP               as Plugin       (Brief = "External Physical Properties",Type="PP");
52
53        N                                               as Integer                              (Brief = "Number of Profile Intervals", Default = 1, Lower = 1, Upper = 100);
54        pi                                      as Real                                 (Brief="pi number",Default=3.141592, Symbol = "\pi");
55        eps                             as Real                                 (Brief="Small Number",Default=1E-8);
56        g                                               as acceleration                 (Brief="Acceleration of gravity");
57        Lpipe                           as length                               (Brief="Pipe Length", Symbol = "L_{pipe}");
58        Hrise                           as angle                                (Brief="Pipe Rise", Symbol = "H_{rise}");
59        Dpipe                           as length                               (Brief="Pipe Inner Diameter", Symbol = "D_{pipe}");
60        Apipe                           as area                                 (Brief="Pipe Area", Symbol = "A_{pipe}");
61        Roughness               as length                               (Brief="Pipe Roughness", Symbol = "\varepsilon");
62        M(NComp)                as molweight            (Brief="Component Mol Weight");
63        FlowRegime              as Switcher                     (Brief="Pipe flow regime",Valid=["laminar","turbulent"],Default="laminar");
64        Correlation             as Switcher                     (Brief="Holdup Correlation for Two Phase Flow", Valid=["Beggs-Brill","Lockhart-Martinelli"], Default="Beggs-Brill");
65        Thermal                         as Switcher                     (Brief="Pipe Thermal Specification ",Valid=["Constant Temperature","Linear Temperature profile"],Default="Constant Temperature");
66        Toutlet                                 as temperature          (Brief= "Outlet Temperature", Symbol = "T_{out}");
67
68SET
69
70        g                       = 1*'ga';
71        Apipe   = 0.25*pi*Dpipe^2;
72        M               = PP.MolecularWeight();
73       
74VARIABLES
75       
76        in              Inlet                   as stream               (Brief = "Inlet Stream" ,PosX=0, PosY=0.5225, Symbol = "^{in}");
77        out     Outlet                  as streamPH     (Brief = "Outlet Stream",PosX=1, PosY=0.5225, Symbol = "^{out}");
78       
79        Liquid          as props                (Brief = "Liquid Properties", Symbol = " ");
80        Vapour     as props                     (Brief = "Vapour Properties", Symbol = " ");
81       
82        Tincr(N+1)      as temperature (Brief = "Temperature Profile", Symbol = "T_{incr}");
83       
84        Pdrop                           as pressure             (Brief = "Total Pressure Drop", DisplayUnit = 'kPa',Lower = 0, Symbol = "\Delta P_{drop}");
85        dPfricTotal             as pressure             (Brief = "Total Friction Pressure Drop", DisplayUnit = 'kPa',Lower = 0, Symbol = "\Delta Ptotal_{fric}");
86        dPelvTotal              as pressure             (Brief = "Total Elevation Pressure Drop", DisplayUnit = 'kPa',Lower = 0 , Symbol = "\Delta Ptotal_{elev}");     
87        dPaccTotal              as pressure             (Brief = "Total Acceleration Pressure Drop", DisplayUnit = 'kPa',Lower = 0 , Symbol = "\Delta Ptotal_{acc}");   
88        dPfric(N+1)             as pressure             (Brief = "Friction Pressure Drop", DisplayUnit = 'kPa',Lower = 0, Symbol = "\Delta P_{fric}");
89        dPelv(N+1)              as pressure             (Brief = "Elevation Pressure Drop", DisplayUnit = 'kPa',Lower = 0 , Symbol = "\Delta P_{elev}");
90        dPacc(N+1)              as pressure             (Brief = "Acceleration Pressure Drop", DisplayUnit = 'kPa',Lower = 0 , Symbol = "\Delta P_{acc}");
91        Pincr(N+1)              as pressure             (Brief = "Pressure Profile", DisplayUnit = 'kPa' , Symbol = "P_{incr}");
92       
93        Lincr(N+1)              as length                       (Brief = "Length Points", Symbol = "L_{incr}");
94        fns(N+1)                        as fricfactor           (Brief = "No Slip Friction Factor");
95        ftp(N+1)                        as fricfactor           (Brief = "Two phase Friction Factor");
96        Mw                                      as molweight    (Brief = "Average Mol Weight");
97        zmass(NComp)    as fraction                     (Brief = "Mass Fraction");
98        Re(N+1)                         as Real                         (Brief = "Reynolds Number Profile");
99        Fw                                      as flow_mass    (Brief = "Total Mass Flow Profile" , Lower = 0,DisplayUnit = 'kg/h', Symbol = "F_w");
100       
101        rho(N+1)                        as dens_mass    (Brief = "Mass Density Profile" , Symbol = "\rho");
102        mu(N+1)                         as viscosity            (Brief = "Viscosity Profile" , Symbol = "\mu");
103        Vel(N+1)                        as velocity             (Brief = "Velocity Profile");
104        vm(N+1)                 as vol_mol              (Brief = "Mixture Molar Volume Profile");
105        h(N+1)                          as enth_mol             (Brief = "Molar Enthalpy profile");
106       
107        dPdLfric(N+1)           as positive             (Brief = "Friction Gradient",Lower = 0, Unit = 'Pa/m', DisplayUnit = 'kPa/m');
108        dPelvdL(N+1)            as positive             (Brief = "Elevation Gradient", Lower = 0 , Unit = 'Pa/m', DisplayUnit = 'kPa/m');
109        #dPaccdL(N+1)           as positive             (Brief = "Acceleration Gradient",Lower = 0 , Unit = 'Pa/m', DisplayUnit = 'kPa/m');
110       
111#Beggs&Brill Method
112#+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
113        NFR(N+1)                                as positive             (Brief="Froude Number", Lower=1E-10,Symbol = "N_{FR}");
114        BBLine1(N+1)                    as positive             (Brief="Beggs and Brill Correlation Parameter 1");
115        BBLine2(N+1)                    as positive             (Brief="Beggs and Brill Correlation Parameter 2");
116        BBLine3(N+1)                    as positive             (Brief="Beggs and Brill Correlation Parameter 3");
117        BBLine4(N+1)                    as positive             (Brief="Beggs and Brill Correlation Parameter 4");
118        Map(N+1)                                as positive             (Brief="Beggs and Brill Flag ");#apenas verificação do algoritmo
119        Atrans(N+1)                             as positive             (Brief="Beggs and Brill Correction When Flow is in Transition Pattern");
120        Y(N+1)                                  as positive             (Brief="Beggs and Brill Correction for Friction Factor in Two Phase Flow");
121        S(N+1)                                  as Real                         (Brief="Beggs and Brill Correction for Friction Factor in Two Phase Flow");
122
123#Lockhart&Martinelli Method
124#+++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++++
125
126XLM(N+1)                                        as Real                         (Brief="Lockhart and Martinelli  Parameter - Square", Lower=1E-6);
127PhiLM(N+1)                              as Real                         (Brief="Lockhart and Martinelli  Two phase Multiplier - Square", Lower=1E-3);
128
129EQUATIONS
130
131"Total Average Molecular Weight"
132        Mw = sum(M*Inlet.z);
133
134"Froude Number"
135        NFR =Vel*Vel/(g*Dpipe);
136
137"No Slip Liquid Volume Fraction"
138        Liquid.Vsfrac = Liquid.Vel/Vel;
139
140"No Slip Vapour Volume Fraction"
141        Vapour.Vsfrac = Vapour.Vel/Vel;
142
143"Vapour Holdup"
144        Vapour.Holdup=1-Liquid.Holdup;
145       
146for i in [1:N+1]
147
148if Vapour.frac(i) equal 0 then # Only Liquid phase
149
150"Reynolds Number"
151        Re(i)*mu(i)     = rho(i)*Vel(i)*Dpipe;
152
153"Liquid Superficial Velocity"
154        Liquid.Vel(i) = Liquid.Fw(i)/Apipe/Liquid.rho(i);
155
156"Vapour Superficial Velocity"
157        Vapour.Vel(i) = 0*'m/s';
158
159"Liquid Mass Flow"
160        Liquid.Fw(i) = Fw;
161
162"Vapour Mass Flow"
163        Vapour.Fw(i) =  0*Fw;
164       
165"Liquid Holdup"
166        Liquid.Holdup(i) = 1;
167
168"Lockhart-martinelli Two Phase Multiplier"
169        XLM(i)  = 1;
170
171        PhiLM(i) = 1;
172       
173"Beggs and Brill Line 1"
174        BBLine1(i) = 1;
175
176"Beggs and Brill Line 2"
177        BBLine2(i) = 1;
178
179"Beggs and Brill Line 3"
180        BBLine3(i) = 1;
181
182"Beggs and Brill Line 4"
183        BBLine4(i) = 1;
184       
185Map(i)=10;     
186Atrans(i) = 1;
187Y(i) = 1;
188
189ftp(i)= 1;
190       
191        S(i)= 1;
192       
193else if Liquid.frac(i) equal 0 then # Only Vapour phase
194
195"Reynolds Number"
196        Re(i)*mu(i)     = rho(i)*Vel(i)*Dpipe;
197
198"Vapour Superficial Velocity"
199        Vapour.Vel(i) = Vapour.Fw(i)/Apipe/Vapour.rho(i);
200
201"Liquid Superficial Velocity"
202        Liquid.Vel(i) = 0*'m/s';
203
204"Liquid Mass Flow"
205        Liquid.Fw(i) = 0*Fw;
206
207"Vapour Mass Flow"
208        Vapour.Fw(i) = Fw;
209
210"Liquid Holdup"
211        Liquid.Holdup(i) = 0;
212
213"Lockhart-martinelli Two Phase Multiplier"
214        XLM(i)  = 1;
215
216        PhiLM(i) = 1;
217       
218"Beggs and Brill Line 1"
219        BBLine1(i) = 1;
220
221"Beggs and Brill Line 2"
222        BBLine2(i) = 1;
223
224"Beggs and Brill Line 3"
225        BBLine3(i) = 1;
226
227"Beggs and Brill Line 4"
228        BBLine4(i) = 1;
229
230Map(i)=11;     
231Atrans(i) = 1;
232Y(i) = 1;
233
234ftp(i)= 1;
235       
236        S(i)= 1;
237       
238else # Two phase
239
240"Reynolds Number"
241        Re(i)*(Liquid.mu(i)*Liquid.Vsfrac(i)+Vapour.mu(i)*Vapour.Vsfrac(i))= (Liquid.rho(i)*Liquid.Vsfrac(i)+Vapour.rho(i)*Vapour.Vsfrac(i))*Vel(i)*Dpipe; #no sip Reynolds Number
242
243"Vapour Superficial Velocity"
244        Vapour.Vel(i) = Vapour.Fw(i)/Apipe/Vapour.rho(i);
245
246"Liquid Superficial Velocity"
247        Liquid.Vel(i) = Liquid.Fw(i)/Apipe/Liquid.rho(i);
248
249"Liquid Mass Flow"
250        Liquid.Fw(i)= Inlet.F*Liquid.frac(i)*sumt(M(1:NComp)*Liquid.Mfrac(i,1:NComp));
251
252"Vapour Mass Flow"
253        Vapour.Fw(i) =  Inlet.F*Vapour.frac(i)*sumt(M(1:NComp)*Vapour.Mfrac(i,1:NComp));
254       
255switch Correlation
256       
257        case "Beggs-Brill":
258
259"Lockhart-martinelli Two Phase Multiplier"
260        XLM(i)  = 1;
261
262        PhiLM(i) = 1;
263       
264"Beggs and Brill Line 1"       
265        BBLine1(i) = 2.499687083 + 0.302*log(Liquid.Vsfrac(i));#aplicado o log somente no lado direito da equação
266
267"Beggs and Brill Line 2"       
268        BBLine2(i) = -3.033764376 - 2.4684*log(Liquid.Vsfrac(i));#aplicado o log somente no lado direito da equação
269
270"Beggs and Brill Line 3"       
271        BBLine3(i) = -1 - 1.4516*log(Liquid.Vsfrac(i));#aplicado o log somente no lado direito da equação
272
273"Beggs and Brill Line 4"       
274        BBLine4(i) = -0.301029996 - 6.738*log(Liquid.Vsfrac(i));#aplicado o log somente no lado direito da equação
275
276Y(i)*Liquid.Holdup(i)*Liquid.Holdup(i) = Liquid.Vsfrac(i);
277
278        ftp(i)= fns(i)*exp(S(i));
279       
280        S(i)= ln(abs(2.2*Y(i)-1.2));
281       
282# Find the Flow Pattern for Beggs-Brill Method
283#++++++++++++++++++++++++++++++++++++++++++
284        if NFR(i) < 10^BBLine1(i) and Liquid.Vsfrac(i) < 0.01
285        then
286        "Liquid Holdup in Segregated Flow"
287        Liquid.Holdup(i)*NFR(i)^0.0868 = 0.98*Liquid.Vsfrac(i)^(0.4846);
288        Atrans(i) = 1;
289        Map(i)=1;
290
291        else
292        if  NFR(i) < 10^BBLine2(i) and Liquid.Vsfrac(i) >= 0.01
293        then
294        "Liquid Holdup in Segregated Flow"
295        Liquid.Holdup(i)*NFR(i)^0.0868 = 0.98*Liquid.Vsfrac(i)^(0.4846);
296        Atrans(i) = 1;
297        Map(i)=1;
298
299        else
300        if NFR(i) > 10^BBLine2(i) and NFR(i) <= 10^BBLine3(i) and Liquid.Vsfrac(i) >= 0.01
301        then
302        "Liquid Holdup in Transition Flow"#usando segregated, deve ser por interpolação!!!
303        Liquid.Holdup(i)*NFR(i)^0.0868 = 0.98*Liquid.Vsfrac(i)^(0.4846);
304       
305        Atrans(i) = abs(10^BBLine3(i) - NFR(i))/(abs(10^BBLine3(i) - 10^BBLine2(i))+eps);
306        Map(i)=2;
307
308        else
309        if NFR(i) > 10^BBLine3(i) and NFR(i) <= 10^BBLine1(i) and Liquid.Vsfrac(i) >= 0.01 and Liquid.Vsfrac(i) < 0.4
310        then
311        "Liquid Holdup in Intermittent Flow"
312        Liquid.Holdup(i)*NFR(i)^0.0173 = 0.845*Liquid.Vsfrac(i)^(0.5351);
313        Atrans(i) = 1;
314        Map(i)=3;
315
316        else
317        if NFR(i) > 10^BBLine3(i) and NFR(i) <= 10^BBLine4(i) and Liquid.Vsfrac(i) >=  0.4
318        then
319        "Liquid Holdup in Intermittent Flow"
320        Liquid.Holdup(i)*NFR(i)^0.0173 = 0.845*Liquid.Vsfrac(i)^(0.5351);
321        Atrans(i) = 1;
322        Map(i)=3;
323
324        else
325        if NFR(i) >= 10^BBLine1(i) and Liquid.Vsfrac(i) <= 0.4
326        then
327        "Liquid Holdup in Distributed Flow"
328        Liquid.Holdup(i)*NFR(i)^0.0609 = 1.065*Liquid.Vsfrac(i)^(0.5824);
329        Atrans(i) = 1;
330        Map(i)=4;
331
332        else
333        if NFR(i) > 10^BBLine4(i) and Liquid.Vsfrac(i) >= 0.4
334        then
335        "Liquid Holdup in Distributed Flow"
336        Liquid.Holdup(i)*NFR(i)^0.0609 = 1.065*Liquid.Vsfrac(i)^(0.5824);
337        Atrans(i) = 1;
338        Map(i)=4;
339
340        else
341        "Outside the Range of Beggs-Brill Method"
342        Liquid.Holdup(i) = Liquid.Vsfrac(i);
343        Atrans(i) = 1;
344        Map(i)=5;
345
346end
347
348end
349
350end
351
352end
353
354end
355
356end
357
358end
359#++++++++++++++++++++++++++++++++++++++++++
360        case "Lockhart-Martinelli":
361       
362"Do Not Use Variables related to Beggs and Brill Method"
363        BBLine1(i) = 1;
364
365"Do Not Use Variables related to Beggs and Brill Method"
366        BBLine2 (i)= 1;
367
368"Do Not Use Variables related to Beggs and Brill Method"
369        BBLine3(i) = 1;
370
371"Do Not Use Variables related to Beggs and Brill Method"
372        BBLine4 (i)= 1;
373
374"Lockhart-martinelli Two Phase Multiplier"
375        XLM(i)*Vapour.rho(i)*Vapour.Vel(i)^2    = Liquid.rho(i)*Liquid.Vel(i)^2;
376       
377        PhiLM(i) = 1+20/sqrt(XLM(i))+1/XLM(i);
378
379"Liquid Holdup"
380        Liquid.Holdup(i) = (1/abs(PhiLM(i)))^(1/3);
381       
382        Atrans(i) = 1;
383       
384        Map(i)=20;
385       
386        Y(i)=1;
387       
388        ftp(i)= 1;
389       
390        S(i)= 1;
391
392end
393
394
395end
396
397end
398
399end
400
401"Mass Fraction"
402        zmass = M*Outlet.z / Mw;       
403
404"Total Mass Flow"
405        Fw = sum(M*Inlet.z)*Inlet.F;
406
407"Inlet Boudary for Temperature Profile"
408        Tincr(1) =  Inlet.T;
409
410"Outlet Boundary for Temperature Profile"
411        Tincr(N+1) = Outlet.T;
412
413"Inlet Boudary for Pressure Profile"
414        Pincr(1) =  Inlet.P;
415
416"Outlet Boundary for Pressure Profile"
417        Pincr(N+1) = Outlet.P;
418
419"Total Pressure Drop"
420        Pdrop = dPfricTotal+ dPelvTotal + dPaccTotal;
421
422"Total Pressure Drop for Friction"
423        dPfricTotal = dPfric(N+1);
424
425"Total Pressure Drop for Elevation"
426        dPelvTotal = dPelv(N+1);
427
428"Total Pressure Drop for Acceleration "
429        dPaccTotal= sum(dPacc);
430
431"Pipe Initial Length"
432        Lincr(1) = 0*'m';
433
434"Outlet Composition"
435        Outlet.z = Inlet.z;
436
437"Molar Balance"
438        Outlet.F = Inlet.F;
439
440"Mixture Velocity"
441        Vel= Vapour.Vel+Liquid.Vel;
442
443"Incremental Acceleration Pressure Drop at Pipe Entry"
444        dPacc(1) = 0*'Pa';
445
446"Incremental Elevation Pressure Drop"
447        dPelv= rho*g*Lincr*sin(Hrise);
448       
449        dPelvdL= rho*g*sin(Hrise);
450
451"Incremental Friction Pressure Drop"
452        #dPfric = (0.5*fns*Lincr*(Liquid.rho*Liquid.Vsfrac+Vapour.rho*Vapour.Vsfrac)*Vel*Vel/Dpipe);
453        dPfric = PhiLM*(0.5*fns*Lincr*(Liquid.rho*Liquid.Vsfrac+Vapour.rho*Vapour.Vsfrac)*Vel*Vel/Dpipe);
454       
455        dPdLfric = (0.5*fns*(Liquid.rho*Liquid.Vsfrac+Vapour.rho*Vapour.Vsfrac)*Vel*Vel/Dpipe);
456       
457for i in [1:N+1]
458
459"Flash Calculation"
460        [Vapour.frac(i), Liquid.Mfrac(i,:), Vapour.Mfrac(i,:)] = PP.FlashPH(Pincr(i), h(i), Inlet.z);
461
462"Liquid Fraction"
463        Liquid.frac(i) = 1-Vapour.frac(i);
464
465"Enthalpy"
466        h(i) = Liquid.frac(i)*Liquid.h(i) + Vapour.frac(i)*Vapour.h(i);
467       
468        Liquid.h(i) = PP.LiquidEnthalpy(Tincr(i),Pincr(i),Liquid.Mfrac(i,:));
469       
470        Vapour.h(i) = PP.VapourEnthalpy(Tincr(i),Pincr(i),Vapour.Mfrac(i,:));
471
472"Density"
473        rho(i) = Liquid.frac(i)*Liquid.rho(i)+Vapour.frac(i)*Vapour.rho(i);
474       
475        Liquid.rho(i) = PP.LiquidDensity(Tincr(i),Pincr(i),Liquid.Mfrac(i,:));
476       
477        Vapour.rho(i) = PP.VapourDensity(Tincr(i),Pincr(i),Vapour.Mfrac(i,:));
478       
479"Viscosiyty"
480       
481        mu(i) = Liquid.frac(i)*Liquid.mu(i)+Vapour.frac(i)*Vapour.mu(i);
482       
483        Liquid.mu(i) = PP.LiquidViscosity(Tincr(i),Pincr(i),Liquid.Mfrac(i,:));
484       
485        Vapour.mu(i) = PP.VapourViscosity(Tincr(i),Pincr(i),Vapour.Mfrac(i,:));
486       
487"Molar Volume"
488        vm(i) = Liquid.frac(i)*Liquid.vm(i)+Vapour.frac(i)*Vapour.vm(i);
489       
490        Liquid.vm(i) = PP.LiquidVolume(Tincr(i),Pincr(i),Liquid.Mfrac(i,:));
491       
492        Vapour.vm(i) = PP.VapourVolume(Tincr(i),Pincr(i),Vapour.Mfrac(i,:));
493
494end
495
496for i in [1:N]
497       
498"Outlet Pressure"
499        Pincr(i+1) = Pincr(1) - (dPfric(i+1) + dPelv(i+1) + dPacc(i+1));
500
501"Incremental Acceleration Pressure Drop"
502        dPacc(i+1) = (Fw/Apipe)^2*(1/rho(i+1)-1/rho(i));
503       
504"Incremental Length"
505        Lincr(i+1) = i*abs(Lpipe)/N;
506
507end
508
509for  i in [1:N]
510
511switch Thermal
512
513        case "Constant Temperature":
514        "Outlet Temperature"
515                Tincr(i+1) = Inlet.T;
516       
517        case "Linear Temperature profile":
518        "Outlet Temperature"
519                Toutlet - Tincr(1) = Lpipe*((Tincr(i+1)-Tincr(i))/(Lincr(i+1)-Lincr(i)));
520
521end
522
523end
524
525for i in [1:N+1]
526
527switch FlowRegime
528
529        case "laminar":
530
531"Friction Factor for Pressure Drop - laminar Flow"
532        fns(i)*Re(i) = 16;
533
534        when Re(i) > 2300 switchto "turbulent";
535
536        case "turbulent":
537
538"Friction Factor  for Pressure Drop - Turbulent Flow"
539        1/sqrt(fns(i))= -2*log(Roughness/Dpipe/3.7+2.51/Re(i)/sqrt(fns(i)));
540
541        when Re(i) <= 2300 switchto "laminar";
542
543end
544 
545end
546
547end
548
549
550FlowSheet Pipe_simples
551
552PARAMETERS
553        PP      as Plugin(Brief="Physical Properties",
554                Type="PP",
555                Components = [ "isobutane", "benzene","n-hexane"],
556                LiquidModel     = "PR",
557                VapourModel     = "PR"
558        );
559
560        NComp   as Integer;
561
562DEVICES
563        Tube as pipe;
564        Feed as simple_source;
565        Storage as simple_sink;
566
567SET
568        NComp  = PP.NumberOfComponents;
569        Tube.N  = 5;
570       
571        #Tube.Thermal ="Constant Temperature";
572        Tube.Thermal ="Linear Temperature profile";
573        Tube.Toutlet  = (80+273.15) * 'K';
574       
575       
576CONNECTIONS
577        Feed.Outlet to Tube.Inlet;
578        Tube.Outlet to Storage.Inlet;
579
580SPECIFY
581        Feed.Outlet.F = 10 * 'kmol/h';
582        Feed.Outlet.P = 3* 'atm';
583        Feed.Outlet.T = (60+273.15) * 'K';
584        Feed.Outlet.z = [0.5,0.2,0.3];
585
586SET
587        Tube.Lpipe = 5*'m';
588        Tube.Hrise =    0*'deg'; # working only in the horizontal , must be updated
589        Tube.Correlation = "Beggs-Brill";
590        #Tube.Correlation = "Lockhart-Martinelli";
591       
592
593        Tube.Dpipe                      = 3*'in';
594        Tube.Roughness  = 4.572E-5*'m';
595       
596        OPTIONS
597        Dynamic = false;
598        #GuessFile="Pipe_simples";
599
600end
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