Giáo trình thiết kế mô phỏng

FT3/SEC 0.151 0.102 0.174 N/A GAL/MIN 67.936 45.762 78.017 N/A STD LIQ RATE, FT3/SEC 0.210 0.114 0.285 N/A SPECIFIC GRAVITY (H2O=1.0) 0.4748 0.5148 0.4333 N/A MOLECULAR WEIGHT 40.142 45.279 31.840 N/A ENTHALPY, BTU/LB -94.877 -15.215 -78.436 N/A CP, BTU/LB-F 0.479 0.567 0.597 N/A DENSITY, LB/FT3 41.114 36.010 44.277 N/A Z (FROM DENSITY) 0.0352 0.1485 0.1048 N/A (1) STANDARD VAPOR VOLUME IS 379.49 FT3/LB-MOLE (60 F AND 14.696 PSIA) ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 59/59 SIMULATION SCIENCES INC. R PAGE P-13 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM SUMMARY 07/29/05 ============================================================================== STREAM ID S9 S10 S11 NAME PHASE VAPOR VAPOR LIQUID ----- TOTAL STREAM ----- RATE, LB-MOL/SEC 0.617 0.617 0.127 M LB/SEC 1.081E-02 1.081E-02 5.950E-03 STD LIQ RATE, FT3/SEC 0.518 0.518 0.191 TEMPERATURE, F 110.000 161.833 29.764 PRESSURE, PSIA 120.000 160.721 125.000 MOLECULAR WEIGHT 17.515 17.515 46.689 ENTHALPY, MM BTU/SEC 1.126E-03 1.403E-03 -1.477E-05 BTU/LB 104.170 129.830 -2.482 MOLE FRACTION LIQUID 0.0000 0.0000 1.0000 REDUCED TEMP (KAYS RULE) 1.6915 1.8455 0.7289 PRES (KAYS RULE) 0.1842 0.2467 0.2038 ACENTRIC FACTOR 0.0158 0.0158 0.1576 WATSON K (UOPK) 17.516 17.516 15.067 STD LIQ DENSITY, LB/FT3 20.847 20.847 31.188 SPECIFIC GRAVITY 0.3343 0.3343 0.5001 API GRAVITY 291.810 291.810 151.452 -------- VAPOR --------- RATE, LB-MOL/SEC 0.617 0.617 N/A M LB/SEC 1.081E-02 1.081E-02 N/A M M3/SEC 8.778E-04 7.154E-04 N/A STD VAP RATE(1), M M3/SEC 6.630E-03 6.630E-03 N/A SPECIFIC GRAVITY (AIR=1.0) 0.605 0.605 N/A MOLECULAR WEIGHT 17.515 17.515 N/A ENTHALPY, BTU/LB 104.170 129.830 N/A CP, BTU/LB-F 0.506 0.523 N/A DENSITY, LB/M M3 12312.378 15106.319 N/A Z (FROM DENSITY) 0.9861 0.9867 N/A -------- LIQUID -------- RATE, LB-MOL/SEC N/A N/A 0.127 M LB/SEC N/A N/A 5.950E-03 FT3/SEC N/A N/A 0.181 GAL/MIN N/A N/A 81.337 STD LIQ RATE, FT3/SEC N/A N/A 0.191 SPECIFIC GRAVITY (H2O=1.0) N/A N/A 0.5001 MOLECULAR WEIGHT N/A N/A 46.689 ENTHALPY, BTU/LB N/A N/A -2.482 CP, BTU/LB-F N/A N/A 0.584 DENSITY, LB/FT3 N/A N/A 32.835 Z (FROM DENSITY) N/A N/A 0.0338 (1) STANDARD VAPOR VOLUME IS 379.49 FT3/LB-MOLE (60 F AND 14.696 PSIA) ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 60/60 Dæûa vaìo caïc säú liãûu kãút quaí trong Program File, ta xaïc âënh âæåüc: 1. Cäng suáút thæûc cuía maïy neïn C1: ÅÍ P-4: Cäng suáút thæûc cuía maïy neïn C1 laì 392,36 HP 2. Thaình pháön, nhiãût âäü vaì aïp suáút cuía caïc doìng saín pháøm khê vaì loíng: Ở P-10: Ta có S10 (sản phẩm khí) S11 (sản phẩm lỏng) FLUID RATES, LB-MOL/SEC 1 N2 0.0589 7.1637E-14 2 METHANE 0.5438 1.7952E-07 3 ETHANE 0.0141 0.0431 4 PROPANE 2.0029E-04 0.0422 5 BUTANE 1.2819E-06 0.0182 6 IBUTANE 1.5859E-06 7.3687E-03 7 IPENTANE 1.1927E-08 5.1369E-03 8 PENTANE 9.0828E-09 6.1047E-03 9 HEXANE 5.0102E-11 3.1268E-03 10 HEPTANE 8.8805E-13 2.3079E-03 TOTAL RATE, LB-MOL/SEC 0.6170 0.1274 TEMPERATURE, F 161.8332 29.7636 PRESSURE, PSIA 160.7205 125.0000 ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 61/61 8.2 Baìi toaïn 2: Mä phoíng thiãút bë taïch khê - loíng 8.2.1 Baìi toaïn Cho vaìo thiãút bë taïch khê loíng mäüt doìng nguyãn liãûu våïi caïc dæî liãûu sau: • Læu læåüng : 100 kmol/h • t = 300C • P = 10 bar • Thaình pháön hoïa hoüc: Meïthane : 13 kmol/h Ethane : 22 kmol/h Propane : 38 kmol/h Butane : 22 kmol/h Pentane : 5 kmol/h Âiãöu kiãûn laìm viãûc cuía thiãút bë taïch: 300C vaì 7 bar Haîy xaïc âënh: 1. Pháön mol bay håi cuía nguyãn liãûu trong âiãöu kiãûn cuía bçnh taïch? 2. Thaình pháön cuía loíng vaì håi ra khoíi thiãút bë taïch? 3. Nàng suáút nhiãût cuía thiãút bë taïch? ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 62/62 8.2.2 Kãút quaí: $ Generated by PRO/II Keyword Generation System $ Generated on: Sun Jul 24 18:48:32 2005 TITLE DIMENSION METRIC, PRES=BAR, STDTEMP=0, STDPRES=1.01325 SEQUENCE SIMSCI CALCULATION RVPBASIS=APIN, TVP=37.778 COMPONENT DATA LIBID 1,METHANE/2,ETHANE/3,PROPANE/4,BUTANE/5,PENTANE, & BANK=PROCESS,SIMSCI THERMODYNAMIC DATA METHOD SYSTEM=SRK, ENTHALPY(L)=LK, SET=SRK01, DEFAULT STREAM DATA PROPERTY STREAM=S1, TEMPERATURE=30, PRESSURE=10, PHASE=M, & RATE(M)=100, COMPOSITION(M)=1,13/2,22/3,38/4,22/5,5 UNIT OPERATIONS FLASH UID=F1 FEED S1 PRODUCT V=S2, W=S3 ISO TEMPERATURE=30, PRESSURE=7 END ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 63/63 SIMULATION SCIENCES INC. R PAGE H-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM CALCULATION HISTORY 07/24/05 ============================================================================== *** PROBLEM SOLUTION BEGINS FEED FLASH COMPLETE UNIT 1 SOLVED - 'F1 ' *** PROBLEM SOLUTION REACHED *** THIS RUN USED 3.12 PRO/II SIMULATION UNITS *** RUN STATISTICS STARTED 18:48:16 07/24/05 NO ERRORS FINISHED 18:48:16 07/24/05 NO WARNINGS RUN TIMES NO MESSAGES INTERACTIVE 0 MIN, 0.00 SEC CALCULATIONS 0 MIN, 0.19 SEC TOTAL 0 MIN, 0.19 SEC ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 64/64 SIMULATION SCIENCES INC. R PAGE I-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT INDEX 07/24/05 ============================================================================== PAGE CONTENTS ------ ---------------------------------------------------------------- 1 COMPONENT DATA 2 CALCULATION SEQUENCE AND RECYCLES 3 FLASH DRUM SUMMARY 4 STREAM MOLAR COMPONENT RATES 5 STREAM SUMMARY ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 65/65 SIMULATION SCIENCES INC. R PAGE P-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COMPONENT DATA 07/24/05 ============================================================================== COMPONENT COMP. TYPE PHASE MOL. WEIGHT DENSITY, KG/M3 --------------------- ----------- ----------- ----------- ----------- 1 METHANE LIBRARY VAP/LIQ 16.043 299.704 2 ETHANE LIBRARY VAP/LIQ 30.070 356.049 3 PROPANE LIBRARY VAP/LIQ 44.097 507.199 4 BUTANE LIBRARY VAP/LIQ 58.124 583.824 5 PENTANE LIBRARY VAP/LIQ 72.151 630.378 COMPONENT NBP CRIT. TEMP. CRIT. PRES. CRIT. VOLM. C C BAR M3/KG-MOL --------------------- ----------- ----------- ----------- ----------- 1 METHANE -161.490 -82.600 46.001 0.0990 2 ETHANE -88.630 32.300 48.839 0.1480 3 PROPANE -42.070 96.670 42.496 0.2030 4 BUTANE -0.500 152.000 37.997 0.2550 5 PENTANE 36.074 196.500 33.691 0.3040 COMPONENT ACEN. FACT. HEAT FORM. G FORM. KCAL/KG-MOL KCAL/KG-MOL --------------------- ----------- ----------- ----------- 1 METHANE 0.01040 -17814.56 -12070.08 2 ETHANE 0.09860 -20066.78 -7672.47 3 PROPANE 0.15290 -24805.58 -5633.13 4 BUTANE 0.20130 -30040.13 -3982.90 5 PENTANE 0.25060 -34982.56 -2040.48 ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 66/66 SIMULATION SCIENCES INC. R PAGE P-3 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT FLASH DRUM SUMMARY 07/24/05 ============================================================================== FLASH ID F1 NAME FEEDS S1 PRODUCTS VAPOR S2 LIQUID S3 TEMPERATURE, C 30.000 PRESSURE, BAR 7.000 PRESSURE DROP, BAR 3.000 MOLE FRAC VAPOR 0.94580 MOLE FRAC LIQUID 0.05420 DUTY, M*KCAL/HR 0.09956 FLASH TYPE ISOTHERMAL ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 67/67 SIMULATION SCIENCES INC. R PAGE P-4 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM MOLAR COMPONENT RATES 07/24/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED VAPOR LIQUID FLUID RATES, KG-MOL/HR 1 METHANE 13.0000 12.9676 0.0324 2 ETHANE 22.0000 21.7330 0.2670 3 PROPANE 38.0000 36.5869 1.4131 4 BUTANE 22.0000 19.5760 2.4240 5 PENTANE 5.0000 3.7169 1.2831 TOTAL RATE, KG-MOL/HR 100.0000 94.5803 5.4197 TEMPERATURE, C 30.0000 30.0000 30.0000 PRESSURE, BAR 10.0000 7.0000 7.0000 ENTHALPY, M*KCAL/HR 0.2869 0.3813 5.1601E-03 MOLECULAR WEIGHT 41.8527 41.0332 56.1538 MOLE FRAC VAPOR 0.7211 1.0000 0.0000 MOLE FRAC LIQUID 0.2789 0.0000 1.0000 ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 68/68 SIMULATION SCIENCES INC. R PAGE P-5 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM SUMMARY 07/24/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED VAPOR LIQUID ----- TOTAL STREAM ----- RATE, KG-MOL/HR 100.000 94.580 5.420 K*KG/HR 4.185 3.881 0.304 STD LIQ RATE, M3/HR 8.620 8.085 0.535 TEMPERATURE, C 30.000 30.000 30.000 PRESSURE, BAR 10.000 7.000 7.000 MOLECULAR WEIGHT 41.853 41.033 56.154 ENTHALPY, M*KCAL/HR 0.287 0.381 5.160E-03 KCAL/KG 68.540 98.238 16.955 MOLE FRACTION LIQUID 0.2789 0.0000 1.0000 REDUCED TEMP (KAYS RULE) 0.8673 0.8766 0.7323 PRES (KAYS RULE) 0.2330 0.1622 0.1807 ACENTRIC FACTOR 0.1380 0.1347 0.1942 WATSON K (UOPK) 15.179 15.289 13.771 STD LIQ DENSITY, KG/M3 485.517 480.022 568.495 SPECIFIC GRAVITY 0.4860 0.4805 0.5691 API GRAVITY 159.655 162.987 117.157 -------- VAPOR --------- RATE, KG-MOL/HR 72.108 94.580 N/A K*KG/HR 2.730 3.881 N/A K*M3/HR 0.160 0.308 N/A NORM VAP RATE(1), K*M3/HR 1.616 2.120 N/A SPECIFIC GRAVITY (AIR=1.0) 1.307 1.417 N/A MOLECULAR WEIGHT 37.861 41.033 N/A ENTHALPY, KCAL/KG 95.813 98.238 N/A CP, KCAL/KG-C 0.459 0.444 N/A DENSITY, KG/K*M3 17009.778 12581.288 N/A Z (FROM DENSITY) 0.8831 0.9058 N/A -------- LIQUID -------- RATE, KG-MOL/HR 27.892 N/A 5.420 K*KG/HR 1.455 N/A 0.304 M3/HR 2.749 N/A 0.552 GAL/MIN 12.105 N/A 2.432 STD LIQ RATE, M3/HR 2.657 N/A 0.535 SPECIFIC GRAVITY (H2O=1.0) 0.5483 N/A 0.5691 MOLECULAR WEIGHT 52.172 N/A 56.154 ENTHALPY, KCAL/KG 17.373 N/A 16.955 CP, KCAL/KG-C 0.611 N/A 0.600 DENSITY, KG/M3 529.312 N/A 550.967 Z (FROM DENSITY) 0.0391 N/A 0.0283 (1) NORMAL VAPOR VOLUME IS 22.414 M3/KG-MOLE (0 C AND 1 ATM) ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 69/69 Tæì kãút quaí cuía Programme file, ta xaïc âënh âæåüc: 1. Pháön mol bay håi cuía nguyãn liãûu trong âiãöu kiãûn cuía bçnh taïch Theo kãút quaí åí P-3: MOLE FRAC VAPOR 0.94580 Váûy: Pháön mol bay håi cuía nguyãn liãûu trong âiãöu kiãûn cuía bçnh taïch laì 0,9458 hay 94,58% 2. Thaình pháön cuía loíng vaì håi ra khoíi thiãút bë taïch: - Trãn Flowsheet, Right-click vaìo doìng S2 vaì S3 ⇒ hiãøn thë cæía säø læûa choün - Choün Display ⇒ xuáút hiãûn cæía säø Stream Style - Choün Properties tæì drop-down list box åí muûc Stream Label Type - Màûc âënh åí muûc Property List laì Materiel Balance List ⇒ seî hiãøn thë tãn, traûng thaïi doìng, nhiãût âäü, aïp suáút, læu læåüng vaì thaình pháön cuía doìng ⇒ OK ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 70/70 3. Nàng suáút nhiãût cuía thiãút bë taïch: Theo kãút quaí åí P-3: DUTY, M*KCAL/HR 0.09956 Váûy: Nàng suáút nhiãût cuía thiãút bë taïch laì 99560 kCal/h 8.3 Baìi toaïn 3: Tênh nhiãût âäü säi cuía mäüt häùn håüp hai pha åí mäüt aïp suáút nháút âënh 8.3.1 Baìi toaïn Nguyãn liãûu coï thaình pháön, aïp suáút vaì nhiãût âäü nhæ baìi toaïn 2, læu læåüng = 5500 kg/h. Haîy xaïc âënh: 1. Nhiãût âäü säi cuía häùn håüp nguyãn liãûu naìy åí aïp suáút 7 bar? 2. Hàòng säú cán bàòng pha cuía caïc cáúu tæí ? 3. Thaình pháön häùn håüp håi cán bàòng våïi loíng? 4. Nàng suáút nhiãût cuía thiãút bë taïch? 8.3.2 Giaíi quyãút baìi toaïn Âãø giaíi quyãút baìi toaïn trãn, ta tiãún haình caïc bæåïc: • Giaí thiãút cho häùn håüp nguyãn liãûu naìy âi vaìo mäüt bçnh taïch laìm viãûc åí aïp suáút laì 7 bar. • Tiãún haình mä phoíng nhæ baìi toaïn 2 • Vç muäún xaïc âënh nhiãût âäü säi cuía häùn håüp ⇒ åí cæía säø Flash Drum, åí muûc Second Specification ⇒ Choün Bubble point åí muûc Unit Specification • Do phaíi xaïc âënh hàòng säú cán bàòng pha cuía caïc cáúu tæí ⇒ åí cæía säø Flash Drum, åí muûc Print Option ⇒ Choün Include Component K - values 8.3.3 Så âäö baìi toaïn ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 71/71 8.3.4 Kãút quaí: $ Generated by PRO/II Keyword Generation System $ Generated on: Sun Jul 24 20:11:07 2005 TITLE PRINT INPUT=REFP, ION=NONE DIMENSION METRIC, PRES=BAR, STDTEMP=0, STDPRES=1.01325 SEQUENCE SIMSCI CALCULATION RVPBASIS=APIN, TVP=37.778 COMPONENT DATA LIBID 1,METHANE/2,ETHANE/3,PROPANE/4,BUTANE/5,PENTANE, & BANK=PROCESS,SIMSCI THERMODYNAMIC DATA METHOD SYSTEM=SRK, ENTHALPY(L)=LK, SET=SRK01, DEFAULT STREAM DATA PROPERTY STREAM=S1, TEMPERATURE=30, PRESSURE=10, PHASE=M, & RATE(WT)=5500.01, COMPOSITION(M)=1,13/2,22/3,38/4,22/5,5 UNIT OPERATIONS FLASH UID=F1, KPRINT FEED S1 PRODUCT W=S3, V=S2 BUBBLE PRESSURE=7 END ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 72/72 SIMULATION SCIENCES INC. R PAGE H-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM CALCULATION HISTORY 07/24/05 ============================================================================== *** PROBLEM SOLUTION BEGINS FEED FLASH COMPLETE UNIT 1 SOLVED - 'F1 ' *** PROBLEM SOLUTION REACHED *** THIS RUN USED 3.12 PRO/II SIMULATION UNITS *** RUN STATISTICS STARTED 20:10:52 07/24/05 NO ERRORS FINISHED 20:10:52 07/24/05 NO WARNINGS RUN TIMES NO MESSAGES INTERACTIVE 0 MIN, 0.00 SEC CALCULATIONS 0 MIN, 0.11 SEC TOTAL 0 MIN, 0.11 SEC ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 73/73 SIMULATION SCIENCES INC. R PAGE I-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT INDEX 07/24/05 ============================================================================== PAGE CONTENTS ------ ---------------------------------------------------------------- 1 FLASH DRUM SUMMARY 2 STREAM MOLAR COMPONENT RATES 3 STREAM SUMMARY ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 74/74 SIMULATION SCIENCES INC. R PAGE P-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT FLASH DRUM SUMMARY 07/24/05 ============================================================================== FLASH ID F1 NAME FEEDS S1 PRODUCTS VAPOR S2 LIQUID S3 TEMPERATURE, C -78.756 PRESSURE, BAR 7.000 PRESSURE DROP, BAR 3.000 MOLE FRAC VAPOR 0.00000 MOLE FRAC LIQUID 1.00000 DUTY, M*KCAL/HR -0.62892 FLASH TYPE BUBBLE-P VAPOR-LIQUID COMPOSITIONS AND K-VALUES FOR UNIT 1, 'F1' COMPONENT VAPOR LIQUID K-VALUE ------------------- ---------- ---------- ---------- 1 METHANE 0.93087 0.13000 7.1605E+00 2 ETHANE 0.05887 0.22000 2.6761E-01 3 PROPANE 0.00969 0.38000 2.5507E-02 4 BUTANE 5.4730E-04 0.22000 2.4877E-03 5 PENTANE 1.8438E-05 0.05000 3.6877E-04 ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 75/75 SIMULATION SCIENCES INC. R PAGE P-2 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM MOLAR COMPONENT RATES 07/24/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED VAPOR LIQUID FLUID RATES, KG-MOL/HR 1 METHANE 17.0838 0.9309 17.0838 2 ETHANE 28.9110 0.0589 28.9110 3 PROPANE 49.9371 9.6926E-03 49.9371 4 BUTANE 28.9110 5.4730E-04 28.9110 5 PENTANE 6.5707 1.8438E-05 6.5707 TOTAL RATE, KG-MOL/HR 131.4135 0.0000 131.4135 TEMPERATURE, C 30.0000 -78.7564 -78.7564 PRESSURE, BAR 10.0000 7.0000 7.0000 ENTHALPY, M*KCAL/HR 0.3770 0.0000 -0.2519 MOLECULAR WEIGHT 41.8527 17.1648 41.8527 MOLE FRAC VAPOR 0.7211 1.0000 0.0000 MOLE FRAC LIQUID 0.2789 0.0000 1.0000 (1) EQUILIBRIUM VAPOR FROM BUBBLE FLASH - STREAM RATE IS ZERO ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 76/76 SIMULATION SCIENCES INC. R PAGE P-3 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM SUMMARY 07/24/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED VAPOR LIQUID ----- TOTAL STREAM ----- RATE, KG-MOL/HR 131.414 0.000 131.414 K*KG/HR 5.500 0.000 5.500 STD LIQ RATE, M3/HR 11.328 0.000 11.328 TEMPERATURE, C 30.000 -78.756 -78.756 PRESSURE, BAR 10.000 7.000 7.000 MOLECULAR WEIGHT 41.853 17.165 41.853 ENTHALPY, M*KCAL/HR 0.377 0.000 -0.252 KCAL/KG 68.540 0.000 -45.809 MOLE FRACTION LIQUID 0.2789 0.0000 1.0000 REDUCED TEMP (KAYS RULE) 0.8673 0.9759 0.5562 PRES (KAYS RULE) 0.2330 0.1517 0.1631 ACENTRIC FACTOR 0.1380 0.0171 0.1380 WATSON K (UOPK) 15.179 19.384 15.179 STD LIQ DENSITY, KG/M3 485.517 308.164 485.517 SPECIFIC GRAVITY 0.4860 0.3085 0.4860 API GRAVITY 159.655 327.219 159.655 -------- VAPOR --------- RATE, KG-MOL/HR 94.759 0.000 N/A K*KG/HR 3.588 0.000 N/A K*M3/HR 0.211 0.000 N/A NORM VAP RATE(2), K*M3/HR 2.124 0.000 N/A SPECIFIC GRAVITY (AIR=1.0) 1.307 0.593 N/A MOLECULAR WEIGHT 37.861 17.165 N/A ENTHALPY, KCAL/KG 95.813 10.123 N/A CP, KCAL/KG-C 0.459 0.504 N/A DENSITY, KG/K*M3 17009.778 7894.784 N/A Z (FROM DENSITY) 0.8831 0.9416 N/A -------- LIQUID -------- RATE, KG-MOL/HR 36.654 N/A 131.414 K*KG/HR 1.912 N/A 5.500 M3/HR 3.613 N/A 8.792 GAL/MIN 15.907 N/A 38.711 STD LIQ RATE, M3/HR 3.491 N/A 11.328 SPECIFIC GRAVITY (H2O=1.0) 0.5483 N/A 0.4860 MOLECULAR WEIGHT 52.172 N/A 41.853 ENTHALPY, KCAL/KG 17.373 N/A -45.809 CP, KCAL/KG-C 0.611 N/A 0.534 DENSITY, KG/M3 529.312 N/A 625.550 Z (FROM DENSITY) 0.0391 N/A 0.0290 (1) EQUILIBRIUM VAPOR FROM BUBBLE FLASH - STREAM RATE IS ZERO (2) NORMAL VAPOR VOLUME IS 22.414 M3/KG-MOLE (0 C AND 1 ATM) ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 77/77 Tæì kãút quaí cuía Programme file, ta xaïc âënh âæåüc: 1. Nhiãût âäü säi cuía häùn håüp nguyãn liãûu naìy åí aïp suáút 7 bar? ÅÍ P -1: FLASH ID F1 NAME FEEDS S1 PRODUCTS VAPOR S2 LIQUID S3 TEMPERATURE, C -78.756 PRESSURE, BAR 7.000 Váûy nhiãût âäü säi cuía häùn håüp nguyãn liãûu naìy åí aïp suáút 7 bar laì -78,7560C 2. Hàòng säú cán bàòng pha cuía caïc cáúu tæí vaì thaình pháön häùn håüp håi cán bàòng våïi loíng? Cuîng åí P - 1, ta tçm âæåüc: VAPOR-LIQUID COMPOSITIONS AND K-VALUES FOR UNIT 1, 'F1' COMPONENT VAPOR LIQUID K-VALUE ------------------- ---------- ---------- ---------- 1 METHANE 0.93087 0.13000 7.1605E+00 2 ETHANE 0.05887 0.22000 2.6761E-01 3 PROPANE 0.00969 0.38000 2.5507E-02 4 BUTANE 5.4730E-04 0.22000 2.4877E-03 5 PENTANE 1.8438E-05 0.05000 3.6877E-04 3. Nàng suáút nhiãût cuía thiãút bë taïch ÅÍ P -1: DUTY, M*KCAL/HR -0.62892 Váûy nàng suáút nhiãût cuía thiãút bë taïch laì -628920 kCal/h ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 78/78 8.4 Baìi toaïn 4: Mä phoíng thaïp taïch propane 8.4.1 Baìi toaïn Tênh cho thaïp Depropanizer våïi caïc dæî liãûu ban âáöu nhæ sau : • Nguyãn liãûu : - nàng suáút : 400 táún/ngaìy - P = 18 bar - coï thaình pháön 40% håi gäöm : 26% khäúi læåüng propane vaì 74 % khäúi læåüng butane • Thaïp : - 22 âéa lyï thuyãút - naûp liãûu åí âéa 11 - aïp suáút âènh : 16,5 bar - tråí læûc : 10 mbar/âéa lyï thuyãút - thiãút bë ngæng tuû hoaìn toaìn - aïp suáút bçnh taïch : 16,2 bar • Chè tiãu cháút læåüng sau : - saín pháøm âènh : coï 1% khäúi læåüng C4 - saín pháøm âaïy : coï 2% khäúi læåüng C3 ⇒ Haîy xaïc âënh : - Chè säú häöi læu ? - Nàng suáút nhiãût cuía thiãút bë âun säi laûi vaì thiãút bë ngæng tuû (MkCal/ngaìy) - Læu læåüng saín pháøm âènh vaì saín pháøm âaïy ? ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 79/79 8.4.2 Så âäö baìi toaïn 8.4.3 Caïc bæåïc mä phoíng 8.4.3.1 Xaïc âënh hãû âån vë âo Choün hãû âån vë METRIC 1 ton = 1014.04 kilograms 2000 pounds = 1 short ton = 0.907 tonne 2240 pounds = 1 long ton = 1.016 tonne ⇒ Choün kg 8.4.3.2 Xaïc âënh thaình pháön cáúu tæí coï trong hãû Hãû 2 cáúu tæí : Propane vaì Butane 8.4.3.3 Læûa choün caïc phæång trçnh nhiãût âäüng thêch håüp Choün hãû GS (Grayson-Streed) ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 80/80 8.4.3.4 Thiãút láûp caïc thiãút bë coï trong så âäö vaì caïc doìng ra vaì vaìo caïc thiãút bë • Thiãút bë : Thaïp ⇒ click choün biãøu tæåüng thaïp tæì floating PFD ⇒ hiãøn thë cæía säø Column Configuration ⇒ nhàõp choün Condenser vaì Reboiler ⇒ nháûp giaï trë 22 åí muûc Number Theoretical Trays ⇒ OK • Caïc doìng : - Thiãút láûp doìng nguyãn liãûu S1 naûp vaìo âéa thæï 11 cuía thaïp ; - Doìng saín pháøm âènh S2 laì doìng loíng âi ra tæì âaïy bçnh taïch sau khi âaî cho häöi læu mäüt pháön vãö âènh thaïp (ngæng tuû hoaìn toaìn) - Doìng saín pháøm âaïy S3 8.4.3.5 Xaïc âënh thaình pháön, traûng thaïi cuía caïc doìng, xaïc âënh caïc dæî liãûu vãö thiãút bë Ta nháûn tháúy ràòng : chè coï doìng S1, thaïp T1 laì âæåüc viãön âoí ⇒ yãu cáöu nháûp dæî liãûu a- Doìng S1 : • Double click doìng S1 ⇒ ⇒ hiãøn thë baíng Stream Data ⇒ ÅÍ muûc Description baûn coï thãø nháûp tãn FEED (nguyãn liãûu) cho doìng naìy ⇒ click choün Flowrate and Composition ⇒ choün Total Fluid Flowrate ⇒ nháûp vaìo giaï trë 400. Chuï yï, læu læåüng nguyãn liãûu âæåüc tênh bàòng táún/ngaìy, maì åí âáy âån vë laì KG-MOL/HR ⇒ click UOM ⇒ xuáút hiãûn baíng Convert Unit of Measure ⇒ choün Mass ⇒ TON ⇒ DAY ⇒ nhàõp Change Units • Nháûp thaình pháön caïc cáúu tæí cuía doìng S1 : Nháûp giaï trë 26 cho cáúu tæí 1 ⇒ nhàõp nuït TAB ⇒ nháûp 74 cho cáúu tæí 2 ⇒ nhàõp OK âãø quay laûi cæía säø chênh Stream Data • Xaïc âënh nhiãût âäü vaì aïp suáút cuía doìng S1 åí muûc Thermal Condition : ÅÍ doìng First Specification ⇒ choün Pressure ⇒ nháûp giaï trë 18. Xong nhàõp choün Liquid Weight Fraction åí muûc Second Specification ⇒ nháûp giaï trë 0.6 ⇒ OK b- Thaïp T1 • Double-click vaìo C1 ⇒ xuáút hiãûn cæía säø Column • ÅÍ muûc Description nháûp tãn DEPROP • Nhàõp choün vaìo ä thæï hai âæåüc viãön âoí Feeds and Products ⇒ xuáút hiãûn cæía säø Column - Feeds and Products ⇒ ÅÍ baíng trãn, xaïc âënh doìng S1 âæåüc naûp vaìo âéa 11 ⇒ ÅÍ baíng dæåïi, våïi doìng S2 ⇒ choün Fixed Rate Draw åí muûc Type of Product ⇒ choün Liquid åí muûc Phase ⇒ nháûp giaï trë 1 åí muûc Tray ⇒ nháûp giaï trë læu læåüng 104 ⇒ Chuï yï, læu læåüng saín pháøm âæåüc tênh bàòng táún/ngaìy, maì åí âáy âån vë laì KG-MOL/HR ⇒ click UOM ⇒ xuáút hiãûn baíng Convert Unit of Measure ⇒ choün Mass ⇒ TON ⇒ DAY ⇒ nhàõp Change Units ⇒ OK ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 81/81 • Nhàõp choün vaìo ä thæï nháút âæåüc viãön âoí Pressure Profile ⇒ xuáút hiãûn cæía säø Column - Pressure Profile ⇒ Nháûp giaï trë 16.5 bar laì aïp suáút åí âéa trãn cuìng cuía thaïp åí muûc Overall Specification ⇒ ÅÍ muûc Pressure Drop ⇒ choün muûc Per Tray ⇒ nháûp giaï trë 0,01 (bar) ⇒ OK âãø tråí vãö cæía säø Column • ÅÍ muûc Condenser : nhàõp choün Bubble Temperature åí muûc Condenser Type ⇒ nháûp giaï trë 16.2 (bar) åí muûc Pressure trong cæía säø Condenser Data • ÅÍ muûc Performance Specification ⇒ - Nhàõp choün ⇒ xuáút hiãûn cæía säø Column - Specifications and Variables ⇒ click vaìo ä choün Add Specifications and Variables ⇒ click vaìo parameter (chæî âoí vaì gaûch dæåïi âoí) trong muûc Specifications ⇒ xuáút hiãûn cæía säø Parameter ⇒ choün Stream åí muûc Stream/Unit vaì choün doìng S3 åí muûc Stream Name laì doìng saín pháøm âaïy cuía thaïp - Click vaìo Parameter (chæî tràõng trãn nãön âoí) ⇒ xuáút hiãûn cæía säø Parameter selection ⇒ choün Composition åí muûc Parameter ⇒ choün PROPANE laì cáúu tæí âáöu vaì cáúu tæí cuäúi ⇒ OK âãø tråí vãö cæía säø Parameter ⇒ nhàõp choün vaìo Mole Fraction ⇒ click UOM ⇒ xuáút hiãûn baíng Convert Unit of Measure ⇒ choün Mass ⇒ Percent ⇒ nhàõp Change Units ⇒ OK : tråí vãö cæía säø Parameter ⇒ OK : hoaìn thaình cæía säø Parameter ⇒ tråí vãö cæía säø Column - Specifications and Variables ⇒ click vaìo Value ⇒ nháûp giaï trë 2 - Nhàõp choün Insert Specification/ Variable ⇒ xuáút hiãûn thãm mäüt Specification 2 - Tiãúp tuûc nhàõp choün Parameter maìu âoí cuîng åí muûc Specifications ⇒ xuáút hiãûn cæía säø Parameter ⇒ choün Stream åí muûc Stream/Unit vaì choün doìng S2 åí muûc Stream Name ⇒ Click vaìo Parameter (chæî tràõng trãn nãön âoí) ⇒ xuáút hiãûn cæía säø Parameter selection ⇒ choün Composition åí muûc Parameter ⇒ choün BUTANE laì cáúu tæí âáöu vaì cáúu tæí cuäúi ⇒ OK âãø tråí vãö cæía säø Parameter ⇒ nhàõp choün vaìo Mole Fraction ⇒ click UOM ⇒ xuáút hiãûn baíng Convert Unit of Measure ⇒ choün Mass ⇒ Percent ⇒ nhàõp Change Units ⇒ OK : tråí vãö cæía säø Parameter ⇒ OK : hoaìn thaình cæía säø Parameter ⇒ tråí vãö cæía säø Column - Specifications and Variables ⇒ click vaìo Value ⇒ nháûp giaï trë 1 - Click vaìo parameter (chæî âoí vaì gaûch dæåïi âoí) trong muûc Variables 1 ⇒ xuáút hiãûn cæía säø Parameter Selection ⇒ Choün Heat Duty (nàng suáút nhiãût) ⇒ ÅÍ muûc Heater choün REBOILER ⇒ OK : quay laûi cæía säø Variables ⇒ OK : quay laûi cæía säø Column - Specifications and Variables ⇒ Tiãúp tuûc Click vaìo parameter (chæî âoí vaì gaûch dæåïi âoí) trong muûc Variables 2 ⇒ xuáút hiãûn cæía säø Parameter Selection ⇒ Choün Heat Duty (nàng suáút nhiãût) ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 82/82 ⇒ ÅÍ muûc Heater choün CONDENSER ⇒ OK : quay laûi cæía säø Variables ⇒ OK : quay laûi cæía säø Column - Specifications and Variables OK : hoaìn thaình viãûc nháûp dæî liãûu cho T1 8.4.3.6 Tiãún haình mä phoíng vaì xem kãút quaí $ Generated by PRO/II Keyword Generation System $ Generated on: Tue Jul 26 15:12:44 2005 TITLE PRINT INPUT=REFP, ION=NONE DIMENSION METRIC, PRES=BAR, STDTEMP=0, STDPRES=1.01325 SEQUENCE SIMSCI CALCULATION RVPBASIS=APIN, TVP=37.778 COMPONENT DATA LIBID 1,PROPANE/2,BUTANE, BANK=PROCESS,SIMSCI THERMODYNAMIC DATA METHOD SYSTEM=GS, SET=GS01, DEFAULT STREAM DATA PROPERTY STREAM=S1, PRESSURE=18, PHASE=M, LFRACTION(WT)=0.6, & RATE(WT)=400000, COMPOSITION(M)=1,26/2,74 UNIT OPERATIONS COLUMN UID=T1 PARAMETER TRAY=22,IO FEED S1,11 PRODUCT OVHD(WT)=S2,100000, BTMS(M)=S3 CONDENSER TYPE=BUBB, PRESSURE=16.2 DUTY 1,1,,CONDENSER/2,22,,REBOILER PSPEC PTOP=16.5, DPTRAY=0.01 PRINT PROPTABLE=PART ESTIMATE MODEL=CONVENTIONAL, RRATIO=3 SPEC STREAM=S2,PCT(WT), COMP=2,WET, VALUE=1 SPEC STREAM=S3,PCT(WT), COMP=1,WET, VALUE=2 VARY DUTY=1,2 REBOILER TYPE=KETTLE END ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 83/83 SIMULATION SCIENCES INC. R PAGE H-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM CALCULATION HISTORY 07/26/05 ============================================================================== *** PROBLEM SOLUTION BEGINS FEED FLASH COMPLETE SCALING 0 FACTORS = 7.160E-01 ERROR = -6.778E-02 SCALING 1 FACTORS = 7.232E-01 ERROR = -6.464E-02 SCALING 2 FACTORS = 8.709E-01 ERROR = 4.160E-03 INNER 0 : E(ENTH+SPEC) = 4.100E-01 CALCULATING NEW MATRIX INNER 1 : E(ENTH+SPEC) = 2.017E-01 ALPHA = 1.0000 INNER 2 : E(ENTH+SPEC) = 7.976E-02 ALPHA = 1.0000 INNER 3 : E(ENTH+SPEC) = 2.838E-02 ALPHA = 1.0000 INNER 4 : E(ENTH+SPEC) = 6.419E-03 ALPHA = 1.0000 ITER 1 E(K) = 1.144E-02 E(ENTH+SPEC) = 6.419E-03 E(SUM) = 1.604E-01 DAMP = 1.000E+00 INNER 0 : E(ENTH+SPEC) = 1.660E-02 INNER 1 : E(ENTH+SPEC) = 6.574E-03 ALPHA = 1.0000 INNER 2 : E(ENTH+SPEC) = 1.651E-03 ALPHA = 1.0000 INNER 3 : E(ENTH+SPEC) = 6.993E-05 ALPHA = 1.0000 ITER 2 E(K) = 1.346E-03 E(ENTH+SPEC) = 6.993E-05 E(SUM) = 1.595E-02 DAMP = 1.000E+00 INNER 0 : E(ENTH+SPEC) = 2.911E-03 INNER 1 : E(ENTH+SPEC) = 1.527E-04 ALPHA = 1.0000 INNER 2 : E(ENTH+SPEC) = 2.738E-05 ALPHA = 1.0000 INNER 3 : E(ENTH+SPEC) = 2.525E-06 ALPHA = 1.0000 ITER 3 E(K) = 0.000E+00 E(ENTH+SPEC) = 2.525E-06 E(SUM) = 9.704E-04 UNIT 1 SOLVED - 'T1 ' *** PROBLEM SOLUTION REACHED *** THIS RUN USED 47.38 PRO/II SIMULATION UNITS *** RUN STATISTICS STARTED 15:11:49 07/26/05 NO ERRORS FINISHED 15:11:50 07/26/05 NO WARNINGS RUN TIMES NO MESSAGES INTERACTIVE 0 MIN, 0.00 SEC CALCULATIONS 0 MIN, 0.21 SEC TOTAL 0 MIN, 0.21 SEC ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 84/84 SIMULATION SCIENCES INC. R PAGE I-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT INDEX 07/26/05 ============================================================================== PAGE CONTENTS ------ ---------------------------------------------------------------- COLUMN SUMMARY 1 UNIT 1, 'T1' 3 TRAY RATES AND DENSITIES 5 STREAM MOLAR COMPONENT RATES 6 STREAM SUMMARY ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 85/85 SIMULATION SCIENCES INC. R PAGE P-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COLUMN SUMMARY 07/26/05 ============================================================================== UNIT 1, 'T1' TOTAL NUMBER OF ITERATIONS IN/OUT METHOD 3 COLUMN SUMMARY ---------- NET FLOW RATES ----------- HEATER TRAY TEMP PRESSURE LIQUID VAPOR FEED PRODUCT DUTIES DEG C BAR KG-MOL/HR M*KCAL/HR ------ ------- -------- -------- -------- --------- --------- --------- --- 1C 47.6 16.20 10899.4 1776.8L - 38.3190 2 48.8 16.50 10895.5 12676.2 3 49.8 16.51 10726.7 12672.3 4 51.7 16.52 10426.7 12503.5 5 55.3 16.53 9992.8 12203.5 6 61.1 16.54 9530.6 11769.6 7 68.4 16.55 9200.0 11307.4 8 75.6 16.56 9054.2 10976.7 9 81.4 16.57 9031.4 10831.0 10 85.4 16.58 9053.8 10808.2 11 87.8 16.59 13199.0 10830.6 7342.6M 12 88.6 16.60 13218.4 7633.2 13 89.6 16.61 13243.0 7652.6 14 90.8 16.62 13273.6 7677.2 15 92.0 16.63 13311.0 7707.8 16 93.4 16.64 13355.2 7745.2 17 94.8 16.65 13405.7 7789.4 18 96.2 16.66 13461.0 7839.9 19 97.6 16.67 13519.9 7895.2 20 99.0 16.68 13579.4 7954.1 21 100.2 16.69 13637.2 8013.7 22R 101.3 16.70 8071.4 5565.8L 28.1602 FEED AND PRODUCT STREAMS TYPE STREAM PHASE FROM TO LIQUID FLOW RATES HEAT RATES TRAY TRAY FRAC KG-MOL/HR M*KCAL/HR ----- ------------ ------ ---- ---- ------ ------------ ------------ FEED S1 MIXED 11 0.5620 7342.55 33.5075 ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 86/86 PROD S2 LIQUID 1 1776.78 2.4950 PROD S3 LIQUID 22 5565.77 20.8536 OVERALL MOLE BALANCE, (FEEDS - PRODUCTS) -7.9936E-12 OVERALL HEAT BALANCE, (H(IN) - H(OUT) ) 8.9387E-05 ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 87/87 SIMULATION SCIENCES INC. R PAGE P-2 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COLUMN SUMMARY 07/26/05 ============================================================================== UNIT 1, 'T1' (Cont) SPECIFICATIONS SPECIFICATION PARAMETER TRAY COMP SPECIFICATION SPECIFIED CALCULATED NUMBER TYPE NO NO TYPE VALUE VALUE ------------- --------- ---- ------ ------------- ---------- ---------- 1 (ACTIVE) STRM S2 1 2 WT PERCENT 1.000E+00 1.000E+00 2 (ACTIVE) STRM S3 22 1 WT PERCENT 2.000E+00 2.000E+00 REFLUX RATIOS -------- REFLUX RATIOS -------- MOLAR WEIGHT STD L VOL --------- --------- --------- REFLUX / FEED STREAM S1 1.4844 1.2045 1.3420 REFLUX / LIQUID DISTILLATE 6.1343 6.1343 6.1343 ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 88/88 SIMULATION SCIENCES INC. R PAGE P-3 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COLUMN SUMMARY 07/26/05 ============================================================================== UNIT 1, 'T1' (Cont) TRAY NET VAPOR RATES AND DENSITIES --------------- RATES --------------- TRAY MW ACTUAL DENS Z FROM NORMAL ACTUAL KG/M3 DENSITY K*KG/HR K*M3/HR K*M3/HR ---- -------- ------------ -------- ----------- ----------- ----------- 2 44.204 36.45367 0.74741 560.333 284.124 15.371 3 44.345 36.44317 0.74822 561.952 284.037 15.420 4 44.642 36.41043 0.74985 558.177 280.253 15.330 5 45.228 36.38064 0.75244 551.942 273.529 15.171 6 46.258 36.45968 0.75520 544.442 263.804 14.933 7 47.758 36.80700 0.75623 540.014 253.443 14.671 8 49.470 37.44251 0.75444 543.015 246.032 14.503 9 51.000 38.17083 0.75094 552.382 242.766 14.471 10 52.126 38.79028 0.74745 563.394 242.256 14.524 11 52.855 39.23045 0.74481 572.454 242.757 14.592 12 53.111 39.40816 0.74375 405.407 171.090 10.287 13 53.416 39.61896 0.74246 408.777 171.526 10.318 14 53.773 39.86539 0.74093 412.823 172.076 10.355 15 54.178 40.14806 0.73914 417.591 172.763 10.401 16 54.624 40.46479 0.73709 423.075 173.600 10.455 17 55.101 40.81009 0.73483 429.207 174.591 10.517 18 55.594 41.17528 0.73241 435.853 175.723 10.585 19 56.086 41.54870 0.72991 442.811 176.963 10.658 20 56.560 41.91877 0.72740 449.885 178.284 10.732 21 57.002 42.27451 0.72498 456.795 179.618 10.805 22 57.403 42.60685 0.72270 463.322 180.913 10.874 ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 89/89 SIMULATION SCIENCES INC. R PAGE P-4 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COLUMN SUMMARY 07/26/05 ============================================================================== UNIT 1, 'T1' (Cont) TRAY NET LIQUID RATES AND DENSITIES --------------- RATES --------------- TRAY MW ACTUAL DENS Z FROM STD LIQ ACTUAL KG/M3 DENSITY K*KG/HR M3/HR M3/HR ---- -------- ------------ -------- ----------- ----------- ----------- 1 44.204 454.920 0.05902 481.793 948.662 1059.073 2 44.368 453.949 0.06024 483.412 949.936 1064.902 3 44.714 454.767 0.06046 479.637 938.558 1054.687 4 45.403 456.349 0.06085 473.402 918.766 1037.368 5 46.624 458.882 0.06149 465.902 891.505 1015.297 6 48.420 461.858 0.06240 461.474 865.666 999.167 7 50.487 464.025 0.06341 464.475 852.732 1000.969 8 52.334 464.707 0.06431 473.841 854.266 1019.657 9 53.685 464.413 0.06497 484.854 863.093 1044.015 10 54.553 463.867 0.06541 493.914 872.299 1064.775 11 55.070 463.398 0.06570 726.866 1277.801 1568.556 12 55.244 463.188 0.06582 730.237 1281.752 1576.544 13 55.447 462.939 0.06596 734.283 1286.552 1586.133 14 55.678 462.647 0.06611 739.051 1292.289 1597.441 15 55.934 462.310 0.06627 744.534 1298.987 1610.466 16 56.208 461.932 0.06644 750.667 1306.592 1625.059 17 56.492 461.520 0.06662 757.313 1314.958 1640.912 18 56.777 461.086 0.06680 764.271 1323.830 1657.544 19 57.053 460.639 0.06697 771.345 1332.978 1674.509 20 57.311 460.204 0.06714 778.255 1342.007 1691.107 21 57.547 459.796 0.06729 784.782 1350.610 1706.805 22 57.757 459.422 0.06744 321.460 552.275 699.705 ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 90/90 SIMULATION SCIENCES INC. R PAGE P-5 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM MOLAR COMPONENT RATES 07/26/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED LIQUID LIQUID FLUID RATES, KG-MOL/HR 1 PROPANE 1909.0633 1763.2672 145.7961 2 BUTANE 5433.4878 13.5127 5419.9751 TOTAL RATE, KG-MOL/HR 7342.5511 1776.7799 5565.7712 TEMPERATURE, C 92.8478 47.6030 101.2840 PRESSURE, BAR 18.0000 16.2000 16.7000 ENTHALPY, M*KCAL/HR 33.5075 2.4950 20.8536 MOLECULAR WEIGHT 54.4770 44.2037 57.7566 MOLE FRAC VAPOR 0.4089 0.0000 0.0000 MOLE FRAC LIQUID 0.5911 1.0000 1.0000 ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 91/91 SIMULATION SCIENCES INC. R PAGE P-6 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM SUMMARY 07/26/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED LIQUID LIQUID ----- TOTAL STREAM ----- RATE, KG-MOL/HR 7342.551 1776.780 5565.771 K*KG/HR 400.000 78.540 321.460 STD LIQ RATE, M3/HR 706.922 154.648 552.275 TEMPERATURE, C 92.848 47.603 101.284 PRESSURE, BAR 18.000 16.200 16.700 MOLECULAR WEIGHT 54.477 44.204 57.757 ENTHALPY, M*KCAL/HR 33.507 2.495 20.854 KCAL/KG 83.769 31.767 64.872 MOLE FRACTION LIQUID 0.5911 1.0000 1.0000 REDUCED TEMP (KAYS RULE) 0.8910 0.8663 0.8837 PRES (KAYS RULE) 0.4596 0.3815 0.4382 ACENTRIC FACTOR 0.1887 0.1533 0.2000 WATSON K (UOPK) 13.751 14.691 13.521 STD LIQ DENSITY, KG/M3 565.833 507.866 582.065 SPECIFIC GRAVITY 0.5664 0.5084 0.5826 API GRAVITY 118.327 146.842 111.360 -------- VAPOR --------- RATE, KG-MOL/HR 3002.482 N/A N/A K*KG/HR 160.002 N/A N/A K*M3/HR 3.683 N/A N/A NORM VAP RATE(1), K*M3/HR 67.298 N/A N/A SPECIFIC GRAVITY (AIR=1.0) 1.840 N/A N/A MOLECULAR WEIGHT 53.290 N/A N/A ENTHALPY, KCAL/KG 119.965 N/A N/A CP, KCAL/KG-C 0.605 N/A N/A DENSITY, KG/K*M3 43449.039 N/A N/A Z (FROM DENSITY) 0.7255 N/A N/A -------- LIQUID -------- RATE, KG-MOL/HR 4340.069 1776.780 5565.771 K*KG/HR 239.998 78.540 321.460 M3/HR 525.730 172.646 699.705 GAL/MIN 2314.717 760.138 3080.705 STD LIQ RATE, M3/HR 421.056 154.648 552.275 SPECIFIC GRAVITY (H2O=1.0) 0.5706 0.5084 0.5826 MOLECULAR WEIGHT 55.298 44.204 57.757 ENTHALPY, KCAL/KG 59.637 31.767 64.872 CP, KCAL/KG-C 0.712 0.715 0.715 DENSITY, KG/M3 456.504 454.920 459.422 Z (FROM DENSITY) 0.0717 0.0590 0.0674 (1) NORMAL VAPOR VOLUME IS 22.414 M3/KG-MOLE (0 C AND 1 ATM) ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 92/92 8.5 Baìi toaïn 5: Xaïc âënh âéa naûp liãûu täúi æu cho thaïp taïch propane bàòng cäng cuû Optimiser 8.5.1 Baìi toaïn Tênh cho thaïp Depropanizer våïi caïc dæî liãûu ban âáöu nhæ sau : • Nguyãn liãûu : - nàng suáút : 400 táún/ngaìy - P = 18 bar - coï thaình pháön 40% håi gäöm : 26% khäúi læåüng propane vaì 74 % khäúi læåüng butane • Thaïp : - 22 âéa lyï thuyãút - aïp suáút âènh : 16,5 bar - tråí læûc : 10 mbar/âéa lyï thuyãút - thiãút bë ngæng tuû hoaìn toaìn ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 93/93 - aïp suáút bçnh taïch : 16,2 bar • Chè tiãu cháút læåüng sau : - saín pháøm âènh : coï 0,5% khäúi læåüng C4 - saín pháøm âaïy : coï 0,5% khäúi læåüng C3 ⇒ Haîy xaïc âënh âéa naûp liãûu täúi æu âãø nàng suáút cuía thiãút bë âun säi laûi laì beï nháút 8.5.2 Sæí duûng cäng cuû Optimiser • Optimiser laì mäüt cäng cuû ráút tiãûn êch cuía PRO/II nhàòm cæûc âaûi hoàûc cæûc tiãøu hoïa mäüt haìm muûc tiãu naìo âoï bàòng caïch thay âäøi giaï trë cuía mäüt biãún naìo âoï trong säú caïc tiãu chuáøn âæa ra • Haìm muûc tiãu coï thãø laì nàng suáút, cäng suáút hoàûc haìm kinh tãú nhæ haìm giaï caí hoàûc haìm chi phê. Vç váûy tuyì theo træåìng håüp maì seî täúi æu haìm muûc tiãu âãún giaï trë cæûc âaûi hoàûc cæûc tiãøu • Biãún seî thay âäøi giaï trë trong mäüt khoaíng naìo âoï (giæîa Minimum Value vaì Maximum Value) âãø haìm muûc tiãu âaût âãún giaï trë cæûc âaûi hoàûc cæûc tiãøu ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 94/94 8.5.3 Giaíi quyãút baìi toaïn • Chuïng ta seî tiãún haình mä phoíng baìi toaïn nhæ baìi toaïn træåïc, sau âoï seî caìi âàût thãm thiãút bë Optimiser OP1 cho thaïp ⇒ OP1 âæåüc viãön âoí • Double-click vaìo OP1 ⇒ hiãøn thë cæía säø PRO/II - Optimiser • ÅÍ muûc Description nháûp tãn OPTIMISER • Goüi cäng cuû Optimiser våïi: o Haìm muûc tiãu: Nàng suáút cuía thiãút bë âun säi laûi o Loaûi baìi toaïn: Cæûc tiãøu (minimize) o Biãún: Vë trê âéa naûp liãûu, biãún thiãn tæì âéa thæï 2 âãún âéa thæï 21 • ÅÍ muûc Objective ⇒ Choün Minimize • ÅÍ muûc Objective Function ⇒ Nhàõp choün Parameter ⇒ hiãøn thë cæía säø Parameter ⇒ ÅÍ muûc Stream/Units ⇒ Choün Column ⇒ Nhàõp choün Parameter ⇒ hiãøn thë cæía säø Parameter Selection ⇒ ÅÍ muûc Parameter choün Heat Duty ⇒ ÅÍ muûc Heater choün Reboiler ⇒ OK : tråí vãö cæía säø Parameter ⇒ OK : tråí vãö cæía säø PRO/II - Optimiser • ÅÍ muûc Variables ⇒ Nhàõp choün Parameter ⇒ hiãøn thë cæía säø Parameter ⇒ ÅÍ muûc Stream/Units ⇒ Choün Column ⇒ Nhàõp choün Parameter ⇒ hiãøn thë cæía säø Parameter Selection ⇒ ÅÍ muûc Parameter choün Tray Location ⇒ ÅÍ muûc Tray Location choün Feed ⇒ ÅÍ muûc Feed Stream choün S1 ⇒ OK : tråí vãö cæía säø Parameter ⇒ OK : tråí vãö cæía säø PRO/II - Optimiser • Tiãúp tuûc åí muûc Variables ⇒ nháûp giaï trë 2 cho muûc Minimum Value vaì giaï trë 22 cho muûc Maximum Value ⇒ nhàõp OK : hoaìn thaình viãûc nháûp dæî liãûu cho OP1 ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 95/95 8.5.4 Tiãún haình mä phoíng vaì xem kãút quaí 8.6 Baìi toaïn 6: Xaïc âënh säú âéa lyï thuyãút täúi thiãøu vaì chè säú häöi læu täúi thiãøu cho thaïp taïch propane bàòng phæång phaïp shortcut 8.6.1 Baìi toaïn Tênh cho thaïp Depropanizer våïi caïc dæî liãûu ban âáöu nhæ sau : • Nguyãn liãûu : - nàng suáút : 400 táún/ngaìy - P = 18 bar - coï thaình pháön 40% håi gäöm : 26% khäúi læåüng propane vaì 74 % khäúi læåüng butane • Thaïp : - aïp suáút âènh : 16,5 bar - tråí læûc : 10 mbar/âéa lyï thuyãút ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 96/96 - thiãút bë ngæng tuû hoaìn toaìn - aïp suáút bçnh taïch : 16,2 bar • Chè tiãu cháút læåüng sau : - saín pháøm âènh : coï 0,5% khäúi læåüng C4 - saín pháøm âaïy : coï 0,5% khäúi læåüng C3 ⇒ Haîy xaïc âënh : - Säú âéa lyï thuyãút täúi thiãøu? - Chè säú häöi læu täúi thiãøu? ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 97/97 8.6.2 Tiãún haình mä phoíng vaì xem kãút quaí $ Generated by PRO/II Keyword Generation System $ Generated on: Mon Aug 15 18:33:48 2005 TITLE DIMENSION METRIC, PRES=BAR, TIME=DAY, STDTEMP=0, STDPRES=1.01325 SEQUENCE SIMSCI CALCULATION RVPBASIS=APIN, TVP=37.778 COMPONENT DATA LIBID 1,PROPANE/2,BUTANE, BANK=PROCESS,SIMSCI THERMODYNAMIC DATA METHOD SYSTEM=GS, SET=GS01, DEFAULT STREAM DATA PROPERTY STREAM=S1, PRESSURE=18, PHASE=M, LFRACTION(WT)=0.6, & RATE(WT)=400000, COMPOSITION(M)=1,26/2,74 UNIT OPERATIONS SHORTCUT UID=SCD1 FEED S1 PRODUCT STREAM=S2, RATE(WT)=1E5, PHASE=L, PRESSURE=16.2 PRODUCT STREAM=S3, PHASE=L, DP=0 CONDENSER TYPE=BUBB EVALUATE MODEL=CONV, TRIAL=50, KEYLIGHT=1, KEYHEAVY=2, RRMIN=2 FINDEX 2 SPEC STREAM=S2,PCT(WT), COMP=2,WET, VALUE=0.5 SPEC STREAM=S3,PCT(WT), COMP=1,WET, VALUE=0.5 END ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 98/98 SIMULATION SCIENCES INC. R PAGE H-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM CALCULATION HISTORY 08/15/05 ============================================================================== *** PROBLEM SOLUTION BEGINS FEED FLASH COMPLETE UNIT 1 SOLVED - 'SCD1 ' *** PROBLEM SOLUTION REACHED *** THIS RUN USED 20.71 PRO/II SIMULATION UNITS *** RUN STATISTICS STARTED 18:33:32 08/15/05 NO ERRORS FINISHED 18:33:33 08/15/05 NO WARNINGS RUN TIMES NO MESSAGES INTERACTIVE 0 MIN, 0.00 SEC CALCULATIONS 0 MIN, 0.12 SEC TOTAL 0 MIN, 0.12 SEC ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 99/99 SIMULATION SCIENCES INC. R PAGE I-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT INDEX 08/15/05 ============================================================================== PAGE CONTENTS ------ ---------------------------------------------------------------- 1 COMPONENT DATA 2 CALCULATION SEQUENCE AND RECYCLES SHORTCUT COLUMN SUMMARY 3 UNIT 1, 'SCD1' 4 STREAM MOLAR COMPONENT RATES 5 STREAM SUMMARY ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 100/100 SIMULATION SCIENCES INC. R PAGE P-1 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT COMPONENT DATA 08/15/05 ============================================================================== COMPONENT COMP. TYPE PHASE MOL. WEIGHT DENSITY KG/M3 --------------------- ----------- ----------- ----------- ----------- 1 PROPANE LIBRARY VAP/LIQ 44.097 507.199 2 BUTANE LIBRARY VAP/LIQ 58.124 583.824 COMPONENT NBP CRIT. TEMP. CRIT. PRES. CRIT. VOLM. C C BAR M3/KG-MOL --------------------- ----------- ----------- ----------- ----------- 1 PROPANE -42.070 96.670 42.496 0.2030 2 BUTANE -0.500 152.000 37.997 0.2550 COMPONENT ACEN. FACT. HEAT FORM. G FORM. KCAL/KG-MOL KCAL/KG-MOL --------------------- ----------- ----------- ----------- 1 PROPANE 0.15290 -24805.58 -5633.13 2 BUTANE 0.20130 -30040.13 -3982.90 ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 101/101 SIMULATION SCIENCES INC. R PAGE P-2 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT CALCULATION SEQUENCE AND RECYCLES 08/15/05 ============================================================================== CALCULATION SEQUENCE SEQ UNIT ID UNIT TYPE --- ------------ ---------- 1 SCD1 SHORTCUT ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 102/102 SIMULATION SCIENCES INC. R PAGE P-3 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT SHORTCUT COLUMN SUMMARY 08/15/05 ============================================================================== UNIT 1, 'SCD1' FEEDS STREAM PHASE ------------ ------ S1 MIXED PRODUCTS ------------- TOTAL STREAM RATES ------------- MOLES WEIGHT LIQUID VOL NORM VAPOR(1) NUM STREAM + PHASE KG-MOL/DAY KG/DAY M3/DAY M3/DAY SECTION TRAYS ------ ------ - ---------- ---------- ---------- ---------- ------- ----- S2 L 1880.26 83014.05 163.56 42144.15 1 13.60 S3 L 5462.28 316985.62 543.36 122431.59 TOTALS 7342.54 399999.66 706.92 164575.74 13.60 SPECIFICATIONS PARAMETER COMP. SPECIFICATION SPECIFIED CALCULATED TYPE NUM TYPE VALUE VALUE ----------------- ------- ------------- ---------- ---------- STRM S2 2 WT PERCENT 5.000E-01 5.001E-01 STRM S3 1 WT PERCENT 5.000E-01 5.000E-01 SUMMARY OF UNDERWOOD CALCULATIONS MINIMUM REFLUX RATIO 3.95841 FEED CONDITION Q 0.59108 FENSKE MINIMUM TRAYS 13.60067 OPERATING REFLUX RATIO 2.00 * R-MINIMUM TOTAL FEED R/R-MIN M/M-MIN REFLUX DUTY, M*KCAL/DAY TRAYS TRAY RATIO CONDENSER REBOILER ----- ---- ------- ------- ------ ---------- ---------- 23 15 1.500 1.657 5.938 -3.924E+01 2.891E+01 21 14 1.750 1.526 6.927 -4.484E+01 3.450E+01 20 13 2.000 1.437 7.917 -5.044E+01 4.010E+01 19 12 2.250 1.372 8.906 -5.604E+01 4.570E+01 18 12 2.500 1.323 9.896 -6.164E+01 5.130E+01 (1) NORMAL VAPOR VOLUME IS 22.414 M3/KG-MOLE (0 C AND 1 ATM) ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 103/103 SIMULATION SCIENCES INC. R PAGE P-4 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM MOLAR COMPONENT RATES 08/15/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED LIQUID LIQUID FLUID RATES, KG-MOL/DAY 1 PROPANE 1909.0616 1873.1184 35.9433 2 BUTANE 5433.4831 7.1424 5426.3407 TOTAL RATE, KG-MOL/DAY 7342.5447 1880.2608 5462.2839 TEMPERATURE, C 92.8478 47.4612 101.2441 PRESSURE, BAR 18.0000 16.2000 16.2000 ENTHALPY, M*KCAL/DAY 33.5076 2.6303 20.5389 MOLECULAR WEIGHT 54.4770 44.1503 58.0317 MOLE FRAC VAPOR 0.4089 0.0000 0.0000 MOLE FRAC LIQUID 0.5911 1.0000 1.0000 ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa Thiãút kãú mä phoíng 104/104 SIMULATION SCIENCES INC. R PAGE P-5 PROJECT PRO/II VERSION 7.0 ELEC V6.6 PROBLEM OUTPUT STREAM SUMMARY 08/15/05 ============================================================================== STREAM ID S1 S2 S3 NAME PHASE MIXED LIQUID LIQUID ----- TOTAL STREAM ----- RATE, KG-MOL/DAY 7342.545 1880.261 5462.284 K*KG/DAY 400.000 83.014 316.986 STD LIQ RATE, M3/DAY 706.922 163.564 543.358 TEMPERATURE, C 92.848 47.461 101.244 PRESSURE, BAR 18.000 16.200 16.200 MOLECULAR WEIGHT 54.477 44.150 58.032 ENTHALPY, M*KCAL/DAY 33.508 2.630 20.539 KCAL/KG 83.768 31.685 64.794 MOLE FRACTION LIQUID 0.5911 1.0000 1.0000 REDUCED TEMP (KAYS RULE) 0.8910 0.8664 0.8814 PRES (KAYS RULE) 0.4596 0.3814 0.4260 ACENTRIC FACTOR 0.1887 0.1531 0.2010 WATSON K (UOPK) 13.751 14.697 13.503 STD LIQ DENSITY, KG/M3 565.833 507.533 583.383 SPECIFIC GRAVITY 0.5664 0.5080 0.5840 API GRAVITY 118.327 147.025 110.812 -------- VAPOR --------- RATE, KG-MOL/DAY 3002.440 N/A N/A K*KG/DAY 160.000 N/A N/A K*M3/DAY 3.682 N/A N/A NORM VAP RATE(1), K*M3/DAY 67.297 N/A N/A SPECIFIC GRAVITY (AIR=1.0) 1.840 N/A N/A MOLECULAR WEIGHT 53.290 N/A N/A ENTHALPY, KCAL/KG 119.965 N/A N/A CP, KCAL/KG-C 0.605 N/A N/A DENSITY, KG/K*M3 43449.017 N/A N/A Z (FROM DENSITY) 0.7255 N/A N/A -------- LIQUID -------- RATE, KG-MOL/DAY 4340.105 1880.261 5462.284 K*KG/DAY 240.000 83.014 316.986 M3/DAY 525.734 182.536 687.057 GAL/MIN 96.447 33.487 126.042 STD LIQ RATE, M3/DAY 421.060 163.564 543.358 SPECIFIC GRAVITY (H2O=1.0) 0.5706 0.5080 0.5840 MOLECULAR WEIGHT 55.298 44.150 58.032 ENTHALPY, KCAL/KG 59.637 31.685 64.794 CP, KCAL/KG-C 0.712 0.715 0.715 DENSITY, KG/M3 456.504 454.782 461.367 Z (FROM DENSITY) 0.0717 0.0590 0.0655 (1) NORMAL VAPOR VOLUME IS 22.414 M3/KG-MOLE (0 C AND 1 ATM) Tæì kãút quaí P-3 cuía Programme file: MINIMUM REFLUX RATIO 3.95841 FENSKE MINIMUM TRAYS 13.60067 Ta xaïc âënh âæåüc: - Säú âéa lyï thuyãút täúi thiãøu: 13,6 - Chè säú häöi læu täúi thiãøu: 3,958 ThS. Lã Thë Nhæ YÏ Âaûi Hoüc Baïch Khoa