oOo - ÌNH LI V À MÁY CH THÁP C-05 C Chuyên ngành :K Mã s : 60 53 55 TÍCH EXERGY ÀNH T LU TP H MINH, tháng 2013 i C ÒA XÃ H -T -H NHI H ên h ên: Chuyên ngành: MSHV: 11400174 B Mã s 605355 ÌNH LI 21-08-1985 K ÀI: V ÀNH T NHI ÀN Kh Mô ph Tính tốn cân b ki So sánh hi -05 C À MÁY CH máy ch -05 c máy cân b -05 gc ành t NGÀY GIAO NHI :( NGÀY HOÀN THÀNH NHI ài): 02/07/2012 ài): 21/06/2013 CÁN B PGS TS NGUY – CÁN B (H ên ch Khoa TP.HCM CH ÀO T (H (H ên ch ên ch ii CƠNG TRÌNH ÀN THÀNH T ÀNH PH Cán b Cán b Cán b Lu … tháng HCM vào ngày Thành ph (Ghi rõ h Xác nh lu CH ên, h àm, h Khoa qu ã ên ngành sau Lu cs ng d tháp C-05 c a nhà máy ch bi n khí Dinh C u ki n v n hành t L ên xin g Nguy c cán b ã quan tâm sâu s nhi ình h àb ài nghiên c Xin chân thành c àn thành Khoa K th óa h ã giúp ,t cho tơi su h bi ã ịng giúp k M ãn ên c ài li th nhiên v b àn thi Cu i cùng, xin g ùng b Tháng 06/2013 H viên th ình Li u Trang Lu cs ng d tháp C-05 c a nhà máy ch bi n khí Dinh C u ki n v n hành t L ày cơng trình nghiên c nhu c ành cơng nghi ên c vào trình nh giá hi qu ày -05 c máy ch bi Các s b ày hồn tồn trung th tác gi ình th ình, b công nh nghi Tp H ình Li u ày 21 tháng 06 Trang Lu cs ng d tháp C-05 c a nhà máy ch bi n khí Dinh C u ki n v n hành t TÓM T S ã mang l , yêu c ùh hát tri ài, gi ành công nghi ch ày t trung vào v ethanizer C-05 c bi Quy trình công ngh c m ên thông s nh hi s Các k thông s cho thi ,n tính ch cơng c mơ ph sau ịng v ành ph c -05 -05 v ã xác c ho nhà máy ch %m thoát exergy cho tháp so v ình Li u Trang Lu cs ng d tháp C-05 c a nhà máy ch bi n khí Dinh C u ki n v n hành t ABSTRACT The development of gas processing industry has brought certain economic achievements as well as assured energy sources In the beginning stage, maximum production requirement is the first priority However, to comply with long term development strategy, technical solution researches for gas processing industry must be focused Base on these matters, this research focuses on energy optimization for Demethanizer C-05 column at Dinh Co gas processing plant Based on actual values of operating parameters, processing stages of this plant was modelled with Hysys software The obtained modelling results were further analyzed to determine properties of process fluids and units as well as energy efficiency of component equipment in C-05 column unit Simultaneously, thermodynamic analysis for C-05 column with Column Targetting tool in Aspen Plus was also conducted to determine necessary adjustments for decreasing more than 98% exergy loss level of the column in comparing with initial operating conditions ình Li u Trang Lu cs ng d tháp C-05 c a nhà máy ch bi n khí Dinh C u ki n v n hành t M L L TÓM T ABSTRACT .4 M DANH M ÌNH DANH M DANH M M T À KÝ HI 11 14 -T NG C À MÁY CH I KHÍ DINH C 16 1.1 GI THI 16 1.2 NGUYÊN LI VÀ S 1.2.1 Nguyên li 1.2.2 Ch 1.3 PH 17 máy 17 s .18 QUY TRÌNH CƠNG NGH C NHÀ MÁY 20 1.3.1 ên lý 20 1.3.2 ình cơng ngh 22 1.4 V NGHIÊN C - TH 2.1 MƠ PH 2.1.1 Mơ ph v .24 VÀ PHÂN TÍCH 25 26 àc -05 26 2.1.1.1 Gi 2.1.1.2 Mô ph ình Li u 26 àc -05 28 Trang Lu cs ng d tháp C-05 c a nhà máy ch bi n khí Dinh C u ki n v n hành t 2.2.2 Phân tích tháp C-05 v 2.2 31 PHÂN TÍCH EXERGY .34 2.2.1 Các m 34 2.2.2 Cân b 2.3 hi PHÂN TÍCH NHI H 37 39 2.3.1 Column Grand Composite Curve (CGCC) 40 2.3.2 Gi .41 -K 3.1 K À BÀN LU QU MÔ PH .43 43 3.1.1 K qu àc 3.1.2 K 3.2 K -05 49 QU TRONG C 3.3 3.4 K -05 43 PHÂN TÍCH EXERGY CHO CÁC THI B THÀNH PH THÁP C-05 54 QU PHÂN TÍCH NHI GIÁ KH -K C À KI TÀI LI H TI 58 63 74 77 PH B BI À MÁY CH À THÁP DEMETHANIZER C-05 PH EXERGY CHO C -05 PH À MÁY CH BI PH NB À MÁY CH ình Li u Trang Lu cs ng d tháp C-05 c a nhà máy ch bi n khí Dinh C u ki n v n hành t DANH M Hình 1 S ên lý nhà máy Hình Ch ng trình tr Hình 2 Nh Hình Dịng v Hình Mơ ph Hình S Hình 3 Bi Hình Thành ph Hình L ul Hình CGCC (T-H) c Hình CGCC (Stage-H) c Hình Bi Hình Bi ÌNH ành hồn ch ình mơ ph cho vi ràng bu 38 máy 46 -05 dịng v Hình 10 Kh 26 33 th -05 c (GPP) 21 50 -05 .58 i (C1- -05 59 -05 .59 -05 61 -Exergy loss c -Exergy loss c -05 61 -05 62 -05 62 òng nh òng nh c -18,50C 65 Hình 11 Kh ràng bu ịng nh òng nh c -600C … 67 Hình 12 Kh ràng bu ịng nh ịng nh c -400 C 69 ình Li u Trang Page of 12 Phase = Liquid TargetType = Phase = Liquid Stage Pressure: StageNumber = / StagePressureValue = 14.98675 bar_g StageNumber = 32 / StagePressureValue = 14.98675 bar_g Specs Summary: SpecName= Propane(bot) / IsActive= True / SpecValue= 0.001 SpecName= Temp top / SpecValue= 46 C SpecName= ibutane / IsActive= True / SpecValue= 0.001 Optional Estimations: Stage = / OptionalTemperatureEstimate = 46 C Stage = 32 / OptionalTemperatureEstimate = 97 C UNIT OPERATION: MIX-100 (Mixer) Feed Stream = gas Feed Stream = 27R Product Stream = mix Pressure Specification=Set to lowest inlet STREAM: 23 (Material Stream) Pressure = 73.98675 bar_g UNIT OPERATION: E-19 (Air cooler) Feed Stream = 23 Product Stream = 24 Pressure Drop = bar NumberOfFans = Fan_Name = Fan STREAM: 24 (Material Stream) Temperature = 50 C UNIT OPERATION: MIX-102 (Mixer) Feed Stream = 24 Feed Stream = gas-6 Product Stream = 25 Pressure Specification=Set to lowest inlet UNIT OPERATION: K-03 (Compressor) Feed Stream = 25 Product Stream = 26 Energy Stream = h25 AdiabaticEfficiency = 85 CompExpCurvesEnabled = UseSurgeCurve = FlowUnits = ACFM UseStonewallCurve = FlowUnits = ACFM OnlyWarn = UseDutySpec = UseAdiabaticEfficiencySpec = UsePolytropicEfficiencySpec = UseDeltaPSpec = file://C:\Documents and Settings\lieupd\Local Settings\Temp\HYSBROW.htm 8/26/2013 Page of 12 UseHeadSpec = UseCapacitySpec = UseSpeedSpec = UseCharacteristicCurves = STREAM: 26 (Material Stream) Pressure = 107.98675 bar_g UNIT OPERATION: K-02 (Compressor) Feed Stream = 22 Product Stream = 23 Energy Stream = h22 AdiabaticEfficiency = 85 CompExpCurvesEnabled = UseSurgeCurve = FlowUnits = ACFM UseStonewallCurve = FlowUnits = ACFM OnlyWarn = UseDutySpec = UseAdiabaticEfficiencySpec = UsePolytropicEfficiencySpec = UseDeltaPSpec = UseHeadSpec = UseCapacitySpec = UseSpeedSpec = UseCharacteristicCurves = UNIT OPERATION: E-13 (Air cooler) Feed Stream = 26 Product Stream = 27 Pressure Drop = bar NumberOfFans = Fan_Name = Fan STREAM: 27 (Material Stream) Temperature = 25.6 C UNIT OPERATION: E-04 (Heat Exchanger) TubeInletStream = 28 TubeOutletStream = 29 ShellInletStream = 36 ShellOutletStream = 37 TEMAType2 = F HCurveName = 28-29 HCurveName = 36-37 ShellPressureDrop = bar TubePressureDrop = bar STREAM: 29 (Material Stream) Temperature = 80 C UNIT OPERATION: K-01 (Compressor) Feed Stream = 30 file://C:\Documents and Settings\lieupd\Local Settings\Temp\HYSBROW.htm 8/26/2013 Page of 12 Product Stream = 31 Energy Stream = h30 AdiabaticEfficiency = 59 CompExpCurvesEnabled = UseSurgeCurve = FlowUnits = ACFM UseStonewallCurve = FlowUnits = ACFM OnlyWarn = UseDutySpec = UseAdiabaticEfficiencySpec = UsePolytropicEfficiencySpec = UseDeltaPSpec = UseHeadSpec = UseCapacitySpec = UseSpeedSpec = UseCharacteristicCurves = STREAM: 31 (Material Stream) Pressure = 45.98675 bar_g UNIT OPERATION: E-17 (Heat Exchanger) TubeInletStream = 34 TubeOutletStream = 35 ShellInletStream = 40 ShellOutletStream = 41 HCurveName = 34-35 HCurveName = 40-41 ShellPressureDrop = bar TubePressureDrop = bar UNIT OPERATION: E-09 (Air cooler) Feed Stream = 37 Product Stream = SP Condensate Pressure Drop = bar NumberOfFans = Fan_Name = Fan STREAM: SP Condensate (Material Stream) Temperature = 45 C STREAM: 41 (Material Stream) Temperature = 60 C UNIT OPERATION: E-12 (Cooler) Feed Stream = 41 Product Stream = SP Butane Energy Stream = h41 Pressure Drop = bar ViewVapourPhase = False ViewLightLiqPhase = False ViewHeavyLiqPhase = False ViewMixedLiqPhase = True file://C:\Documents and Settings\lieupd\Local Settings\Temp\HYSBROW.htm 8/26/2013 Page of 12 STREAM: SP Butane (Material Stream) Temperature = 45 C UNIT OPERATION: K-100 (Expander) Feed Stream = Product Stream = Energy Stream = h4 AdiabaticEfficiency = 58.49 CompExpCurvesEnabled = UseSurgeCurve = UseStonewallCurve = OnlyWarn = UseDutySpec = UseAdiabaticEfficiencySpec = UsePolytropicEfficiencySpec = UseDeltaPSpec = UseHeadSpec = UseCapacitySpec = UseSpeedSpec = UseCharacteristicCurves = STREAM: 32R (Material Stream) Temperature = 42.7556209 C Pressure = 45.98675 bar_g Molar Flow = 1448.57911 kgmole/h Composition Basis (In Mole Fractions): Nitrogen = 0.000291783532 / CO2 = 0.000806818954 / Methane = 0.342439329 / Ethane = 0.526130303 / Propane = 0.10641729 / i-Butane = 0.0103318202 / n-Butane = 0.0108419453 / i-Pentane = 0.00123339454 / n-Pentane = 0.00108392595 / n-Hexane = 0.000246254337 / n-Heptane = 4.15918487e-005 / n-Octane = 9.41403508e-006 / n-Nonane = 1.40813502e-006 / n-Decane = 1.81059758e-007 / Cyclopentane = 5.55892795e-005 / Mcyclopentan = 2.3140385e-005 / Cyclohexane = 1.69023093e-005 / Mcyclohexane = 9.18848441e-006 / Benzene = 1.97052927e-005 / H2O = 6.30468285e-009 / TEGlycol = 9.01125694e-009 / UNIT OPERATION: RCY-1 (Recycle) Inlet Stream = 27 Output Stream = 27R STREAM: 27R (Material Stream) Temperature = 25.6 C Pressure = 107.98675 bar_g Molar Flow = 1708.90468 kgmole/h Composition Basis (In Mole Fractions): Nitrogen = 0.000615487186 / CO2 = 0.000805836257 / Methane = 0.460447769 / Ethane = 0.394054766 / Propane = 0.0942562283 / i-Butane = 0.0153764443 / n-Butane = 0.0208703229 / i-Pentane = 0.00441627678 / n-Pentane = 0.00472489661 / n-Hexane = 0.00218664071 / n-Heptane = 0.000708096951 / n-Octane = 0.000299795001 / n-Nonane = 8.03611696e-005 / n-Decane = 1.79844395e-005 / Cyclopentane = 0.000294663021 / Mcyclopentan = 0.000210912151 / Cyclohexane = 0.000159980553 / Mcyclohexane = 0.000141047063 / Benzene = 0.000174931198 / H2O = 0.000157553528 / TEGlycol = 7.30687919e-009 / UNIT OPERATION: RCY-2 (Recycle) Inlet Stream = 32 Output Stream = 32R file://C:\Documents and Settings\lieupd\Local Settings\Temp\HYSBROW.htm 8/26/2013 Page of 12 STREAM: 35R (Material Stream) Temperature = 45.3615096 C Pressure = 9.98675 bar_g Molar Flow = 807.097943 kgmole/h Composition Basis (In Mole Fractions): Nitrogen = 1.79817597e-016 / CO2 = 4.19258848e-009 / Methane = 3.50420523e-009 / Ethane = 0.0242971264 / Propane = 0.581565899 / i-Butane = 0.146607695 / n-Butane = 0.21067383 / i-Pentane = 0.0203267154 / n-Pentane = 0.0158877231 / n-Hexane = 8.52750749e-005 / n-Heptane = 2.44251453e-008 / n-Octane = 8.04893394e-012 / nNonane = 2.17816194e-015 / n-Decane = 5.8900809e-019 / Cyclopentane = 0.000540172904 / Mcyclopentan = 6.41772809e-006 / Cyclohexane = 1.4086187e-006 / Mcyclohexane = 8.19778395e-009 / Benzene = 7.69627902e-006 / H2O = 3.75366123e-013 / TEGlycol = 1.35107169e-015 / UNIT OPERATION: RCY-3 (Recycle) Inlet Stream = 35 Output Stream = 35R FLOWSHEET: COL2 (Owned By: C-01) FLUID PACKAGE: Basis-1 UNIT OPERATION: Main TS (Tray Section) StageNumber = 20 (Feed)/ NumberOfColumnStages = 32 StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = 10 StgNumber = 11 StgNumber = 12 StgNumber = 13 StgNumber = 14 StgNumber = 15 StgNumber = 16 StgNumber = 17 StgNumber = 18 StgNumber = 19 StgNumber = 20 StgNumber = 21 StgNumber = 22 StgNumber = 23 StgNumber = 24 StgNumber = 25 StgNumber = 26 StgNumber = 27 file://C:\Documents and Settings\lieupd\Local Settings\Temp\HYSBROW.htm 8/26/2013 Page of 12 StgNumber = 28 StgNumber = 29 StgNumber = 30 StgNumber = 31 UNIT OPERATION: Reboiler (Reboiler) Feed Stream = To Reboiler @COL2 Vapour Product = Boilup @COL2 Liquid Product = @COL2 Energy Stream = h9 @COL2 Volume = m3 HeatExchanger = Duty ViewVapourPhase = False ViewLightLiqPhase = False ViewHeavyLiqPhase = False FLOWSHEET: COL3 (Owned By: C-05) FLUID PACKAGE: Basis-1 UNIT OPERATION: TS-1 (Tray Section) NumberOfColumnStages = 12 StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = 10 StgNumber = 11 FLOWSHEET: COL1 (Owned By: T-100) FLUID PACKAGE: Basis-1 UNIT OPERATION: TS-1 (Tray Section) NumberOfColumnStages = StgNumber = StgNumber = StgNumber = StgNumber = FLOWSHEET: COL4 (Owned By: C-02) file://C:\Documents and Settings\lieupd\Local Settings\Temp\HYSBROW.htm 8/26/2013 Page 10 of 12 FLUID PACKAGE: Basis-1 UNIT OPERATION: Main TS (Tray Section) StageNumber = 10 (Feed)/ NumberOfColumnStages = 30 StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = 10 StgNumber = 11 StgNumber = 12 StgNumber = 13 StgNumber = 14 StgNumber = 15 StgNumber = 16 StgNumber = 17 StgNumber = 18 StgNumber = 19 StgNumber = 20 StgNumber = 21 StgNumber = 22 StgNumber = 23 StgNumber = 24 StgNumber = 25 StgNumber = 26 StgNumber = 27 StgNumber = 28 StgNumber = 29 UNIT OPERATION: Condenser (Total Condenser) Feed Stream = To Condenser @COL4 Liquid Product = 34 @COL4 Energy Stream = h34 @COL4 Volume = m3 HeatExchanger = Duty ViewVapourPhase = False ViewLightLiqPhase = False ViewHeavyLiqPhase = False UNIT OPERATION: Reboiler (Reboiler) Feed Stream = To Reboiler @COL4 Vapour Product = Boilup @COL4 Liquid Product = 36 @COL4 Energy Stream = h36 @COL4 Volume = m3 HeatExchanger = Duty ViewVapourPhase = False ViewLightLiqPhase = False file://C:\Documents and Settings\lieupd\Local Settings\Temp\HYSBROW.htm 8/26/2013 Page 11 of 12 ViewHeavyLiqPhase = False FLOWSHEET: COL5 (Owned By: C-04) FLUID PACKAGE: Basis-1 UNIT OPERATION: TS-1 (Tray Section) NumberOfColumnStages = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = FLOWSHEET: COL6 (Owned By: C-03) FLUID PACKAGE: Basis-1 UNIT OPERATION: Main TS (Tray Section) StageNumber = 14 (Feed)/ NumberOfColumnStages = 30 StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = StgNumber = 10 StgNumber = 11 StgNumber = 12 StgNumber = 13 StgNumber = 14 StgNumber = 15 StgNumber = 16 StgNumber = 17 StgNumber = 18 StgNumber = 19 StgNumber = 20 StgNumber = 21 StgNumber = 22 StgNumber = 23 StgNumber = 24 StgNumber = 25 StgNumber = 26 StgNumber = 27 file://C:\Documents and Settings\lieupd\Local Settings\Temp\HYSBROW.htm 8/26/2013 Page 12 of 12 StgNumber = 28 StgNumber = 29 UNIT OPERATION: Condenser (Total Condenser) Feed Stream = To Condenser @COL6 Liquid Product = 39 @COL6 Energy Stream = h39 @COL6 Volume = m3 HeatExchanger = Duty ViewVapourPhase = False ViewLightLiqPhase = False ViewHeavyLiqPhase = False UNIT OPERATION: Reboiler (Reboiler) Feed Stream = To Reboiler @COL6 Vapour Product = Boilup @COL6 Liquid Product = 40 @COL6 Energy Stream = h40 @COL6 Volume = m3 HeatExchanger = Duty ViewVapourPhase = False ViewLightLiqPhase = False ViewHeavyLiqPhase = False file://C:\Documents and Settings\lieupd\Local Settings\Temp\HYSBROW.htm 8/26/2013 Thông tin tính ch t dịng khí ngun li u cung c p t m B ch H m t s o: Stt Tên c Mole % Mole % Mole % 6,0 1,0 2,0 H2S (ppm) Nitrogen (N2) 1,116 0,402 1,110 Cacbon dioxide (CO2) 0,093 0,212 0,095 Methane (CH4) 68,905 70,860 73,052 Ethane (C2H6) 12,518 13,698 12,269 Propane 10,191 9,041 8,624 Iso-Butane 1,839 1,671 1,447 n-Butane 2,802 2,470 2,106 Neo Pentane 0,009 0,009 0,006 10 Iso-Pentane 0,682 0,501 0,428 11 n-Pentane 0,724 0,507 0,421 12 Hexanes 0,578 0,371 0,282 13 Heptanes 0,324 0,167 0,120 14 Octanes 0,112 0,047 0,027 15 Nonanes 0,071 0,027 0,010 16 Decanes 0,024 0,010 0,001 17 Undecanes 0,011 0,006 0,000 18 Dodecanes Plus (C12+) 0,001 0,001 0,000 19 H2O (mg/m3) 3,8 3,4 1,6 - - - 100,000 100,000 100,000 20 T Material stream information: Parameters Vapour Fraction Unit Temperature Pressure Molar Flow Mass Flow Liquid Volume Flow Heat Flow Molar Enthalpy C bar_g kgmole/h kg/h m3/h kJ/h kJ/kgmole feed 0.895 25.6 108.0 7579.0 178751.7 481.9 gas 1.000 25.6 108.0 6783.3 152663.6 426.3 liquid 0.000 25.6 108.0 795.7 26088.1 55.6 gas-6 1.000 20.0 74.0 234.2 4972.6 14.4 0.000 -19.7 32.5 1992.8 76203.0 165.9 water 20 0.000 0.000 20.0 20.0 74.0 74.0 95.0 466.5 1711.4 19404.1 1.7 39.5 33 0.000 107.8 28.0 980.6 55019.4 97.3 21 0.124 41.0 74.0 466.5 19404.1 39.5 liquid-1 0.286 18.5 74.0 795.7 26088.1 55.6 TEG_feed TEG_out 0.000 0.000 26.0 24.8 108.0 108.0 40.0 45.5 6006.8 6121.0 5.3 5.5 1.000 24.8 108.0 8486.7 198006.8 548.3 1.000 24.8 108.0 2546.0 59402.0 164.5 1.000 24.8 108.0 5940.7 138604.7 383.8 0.000 -35.0 108.0 2546.0 59402.0 164.5 0.825 -18.5 32.5 5940.7 138604.7 383.8 684151099.4 581787194.2 102363905.3 -19418686.8 232813208.6 -27214633.1 -55595839.3 126919050.8 -54295041.2 102363905.3 -31838791.3 -33021731.6 737582929.6 221274878.9 516308050.7 236623291.0 521866926.5 Molar Entropy kJ/kgmoleC -90269.8 137.4 -85767.8 140.1 -128649.9 114.7 -82908.8 146.3 -116828.6 102.4 -286483.4 -119185.5 52.3 114.3 -129432.5 126.6 -116396.9 123.5 -128649.9 115.7 -795969.8 -726341.2 143.4 137.9 -86910.2 139.7 -86910.2 139.7 -86910.2 139.7 -92938.6 117.2 -87845.9 142.4 Parameters Vapour Fraction Temperature Pressure Molar Flow Mass Flow Liquid Volume Flow 0.000 -19.7 32.5 1992.8 76203.0 165.9 Sale gas 1.000 11.1 32.5 6494.0 121803.7 382.4 1.000 -40.1 32.5 6494.0 121803.7 382.4 3v 0.473 -62.6 32.5 2546.0 59402.0 164.5 3e 0.507 -60.0 32.5 2546.0 59402.0 164.5 mix 1.000 24.6 108.0 8492.2 198121.0 548.5 22 1.000 44.7 46.0 1474.4 40474.5 107.8 23 1.000 78.2 74.0 1474.4 40474.5 107.8 24 1.000 50.0 74.0 1474.4 40474.5 107.8 25 1.000 45.9 74.0 1708.6 45447.1 122.2 26 1.000 71.1 108.0 1708.6 45447.1 122.2 27 0.000 25.6 108.0 1708.6 45447.1 122.2 28 29 0.000 0.519 40.2 80.0 46.0 46.0 440.7 440.7 18743.9 18743.9 39.8 39.8 30 1.000 15.2 28.0 1452.9 39927.5 108.4 31 1.000 55.0 46.0 1452.9 39927.5 108.4 34 0.000 42.9 10.0 807.1 40196.5 75.1 35 0.166 45.4 10.0 807.1 40196.5 75.1 36 0.000 155.0 10.0 173.5 14823.0 22.2 Heat Flow 232813208.6 509440181.6 524788593.7 236623291.0 235735069.1 738765518.6 128132817.7 126533985.4 130285860.1 149704546.9 148433992.5 156946285.7 -51302561.2 -47763922.6 126416091.0 124199084.7 104950490.9 102726561.7 -28152615.6 Molar Enthalpy Molar Entropy -116828.6 102.4 -78448.4 156.2 -80811.9 147.0 -92938.6 120.3 -92589.7 122.0 -86993.5 139.7 -86906.5 160.1 -85822.1 160.6 -88366.8 153.0 -87618.6 152.4 -86875.0 152.7 -91857.0 137.1 -116419.9 -108389.7 126.1 150.2 -87011.7 161.6 -85485.8 163.5 -130029.4 97.5 -127274.1 106.2 -162307.9 141.3 10.0 Molar Flow 173.5 Mass Flow 14823.0 Liquid Volume Flow 22.2 45.0 10.0 173.5 14823.0 0.000 0.000 0.000 0.000 43.0 99.9 60.0 45.0 15.0 15.0 15.0 15.0 489.2 317.9 317.9 317.9 32R 1.000 42.8 46.0 32 1.000 42.8 27R 0.000 35R 0.166 Parameters 37 SP Condensate SP Propane 40 41 SP Butane Vapour Fraction 0.000 -31691254.2 Molar Enthalpy -182709.1 Molar Entropy 88.1 22.2 -32380395.7 -186682.2 76.0 21303.4 18891.6 18891.6 18891.6 42.5 32.6 32.6 32.6 -116716.2 -140601.9 -147597.2 -149919.9 101.1 106.6 86.8 79.7 1448.6 39814.3 108.1 -86388.8 160.7 46.0 1452.9 39927.5 108.4 -86381.1 160.7 25.6 108.0 1708.9 45457.4 122.2 -91859.0 137.1 45.4 10.0 807.1 40195.1 75.1 -57095276.6 -44699805.2 -46923734.4 -47662131.6 125141044.8 125499882.8 156978324.5 102722823.0 -127274.3 106.2 Temperature Pressure 65.2 0.000 Heat Flow Energy information: Parameter Heat Flow Unit kJ/h h9 27240636 heat-1 134746 h3v h4 h22 h25 h30 h34 h36 h39 h40 h41 888221.9 5558876 1598832 1270554 2217006 18536669 12352623 28282231 29212389 738397.3 Composition information: Comp Mole Frac Nitrogen CO2 C1 C2 C3 i-C4 n-C4 i-C5 n-C5 n-C6 n-C7 n-C8 n-C9 n-C10 Cyclopentane Mcyclopentan Cyclohexane Mcyclohexane Benzene H2O TEGlycol feed 0.0021 0.0006 0.7085 0.1341 0.0750 0.0165 0.0237 0.0063 0.0073 0.0051 0.0026 0.0018 0.0008 0.0003 0.0005 0.0005 0.0004 0.0005 0.0004 0.0130 0.0000 gas 0.0023 0.0006 0.7418 0.1329 0.0697 0.0144 0.0201 0.0049 0.0055 0.0033 0.0014 0.0008 0.0003 0.0001 0.0004 0.0003 0.0002 0.0003 0.0002 0.0005 0.0000 liquid 0.0008 0.0005 0.4243 0.1442 0.1199 0.0342 0.0545 0.0182 0.0227 0.0205 0.0128 0.0105 0.0053 0.0022 0.0017 0.0021 0.0017 0.0025 0.0017 0.1197 0.0000 gas-6 0.0020 0.0007 0.7675 0.1362 0.0607 0.0106 0.0138 0.0028 0.0029 0.0013 0.0004 0.0002 0.0000 0.0000 0.0002 0.0001 0.0001 0.0001 0.0001 0.0004 0.0000 0.0002 0.0005 0.2262 0.2912 0.2687 0.0590 0.0832 0.0202 0.0225 0.0131 0.0054 0.0029 0.0010 0.0003 0.0015 0.0012 0.0010 0.0010 0.0010 0.0000 0.0000 water 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 1.0000 0.0000 20 0.0004 0.0005 0.3384 0.1776 0.1741 0.0529 0.0860 0.0297 0.0374 0.0343 0.0217 0.0178 0.0090 0.0037 0.0029 0.0035 0.0029 0.0042 0.0028 0.0004 0.0000 33 0.0000 0.0000 0.0000 0.0200 0.4787 0.1207 0.1769 0.0481 0.0560 0.0393 0.0201 0.0139 0.0062 0.0023 0.0038 0.0039 0.0031 0.0039 0.0030 0.0000 0.0000 21 0.0004 0.0005 0.3384 0.1776 0.1741 0.0529 0.0860 0.0297 0.0374 0.0343 0.0217 0.0178 0.0090 0.0037 0.0029 0.0035 0.0029 0.0042 0.0028 0.0004 0.0000 liquid-1 0.0008 0.0005 0.4243 0.1442 0.1199 0.0342 0.0545 0.0182 0.0227 0.0205 0.0128 0.0105 0.0053 0.0022 0.0017 0.0021 0.0017 0.0025 0.0017 0.1197 0.0000 TEG_feed 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 1.0000 TEG_out 0.0006 0.0003 0.0234 0.0110 0.0049 0.0003 0.0004 0.0001 0.0001 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0015 0.0777 0.8798 0.0019 0.0007 0.6855 0.1855 0.0747 0.0146 0.0203 0.0048 0.0053 0.0031 0.0013 0.0007 0.0002 0.0001 0.0003 0.0003 0.0002 0.0002 0.0002 0.0000 0.0000 0.0019 0.0007 0.6855 0.1855 0.0747 0.0146 0.0203 0.0048 0.0053 0.0031 0.0013 0.0007 0.0002 0.0001 0.0003 0.0003 0.0002 0.0002 0.0002 0.0000 0.0000 0.0019 0.0007 0.6855 0.1855 0.0747 0.0146 0.0203 0.0048 0.0053 0.0031 0.0013 0.0007 0.0002 0.0001 0.0003 0.0003 0.0002 0.0002 0.0002 0.0000 0.0000 0.0019 0.0007 0.6855 0.1855 0.0747 0.0146 0.0203 0.0048 0.0053 0.0031 0.0013 0.0007 0.0002 0.0001 0.0003 0.0003 0.0002 0.0002 0.0002 0.0000 0.0000 0.0019 0.0007 0.6855 0.1855 0.0747 0.0146 0.0203 0.0048 0.0053 0.0031 0.0013 0.0007 0.0002 0.0001 0.0003 0.0003 0.0002 0.0002 0.0002 0.0000 0.0000 0.0002 0.0005 0.2262 0.2912 0.2687 0.0590 0.0832 0.0202 0.0225 0.0131 0.0054 0.0029 0.0010 0.0003 0.0015 0.0012 0.0010 0.0010 0.0010 0.0000 0.0000 Sale gas 0.0024 0.0007 0.8265 0.1531 0.0152 0.0010 0.0009 0.0001 0.0001 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0024 0.0007 0.8265 0.1531 0.0152 0.0010 0.0009 0.0001 0.0001 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 3v 0.0019 0.0007 0.6855 0.1855 0.0747 0.0146 0.0203 0.0048 0.0053 0.0031 0.0013 0.0007 0.0002 0.0001 0.0003 0.0003 0.0002 0.0002 0.0002 0.0000 0.0000 3e 0.0019 0.0007 0.6855 0.1855 0.0747 0.0146 0.0203 0.0048 0.0053 0.0031 0.0013 0.0007 0.0002 0.0001 0.0003 0.0003 0.0002 0.0002 0.0002 0.0000 0.0000 mix 0.0019 0.0007 0.6852 0.1855 0.0747 0.0146 0.0202 0.0048 0.0053 0.0031 0.0013 0.0007 0.0002 0.0001 0.0003 0.0003 0.0002 0.0002 0.0002 0.0004 0.0000 22 0.0004 0.0008 0.4117 0.4350 0.0996 0.0161 0.0220 0.0047 0.0050 0.0023 0.0008 0.0003 0.0001 0.0000 0.0003 0.0002 0.0002 0.0002 0.0002 0.0001 0.0000 23 0.0004 0.0008 0.4117 0.4350 0.0996 0.0161 0.0220 0.0047 0.0050 0.0023 0.0008 0.0003 0.0001 0.0000 0.0003 0.0002 0.0002 0.0002 0.0002 0.0001 0.0000 24 0.0004 0.0008 0.4117 0.4350 0.0996 0.0161 0.0220 0.0047 0.0050 0.0023 0.0008 0.0003 0.0001 0.0000 0.0003 0.0002 0.0002 0.0002 0.0002 0.0001 0.0000 25 0.0006 0.0008 0.4605 0.3940 0.0942 0.0154 0.0209 0.0044 0.0047 0.0022 0.0007 0.0003 0.0001 0.0000 0.0003 0.0002 0.0002 0.0001 0.0002 0.0002 0.0000 Comp Mole Frac Nitrogen CO2 C1 C2 C3 i-C4 n-C4 i-C5 n-C5 n-C6 n-C7 n-C8 n-C9 n-C10 Cyclopentane Mcyclopentan Cyclohexane Mcyclohexane Benzene H2O TEGlycol 26 0.0006 0.0008 0.4605 0.3940 0.0942 0.0154 0.0209 0.0044 0.0047 0.0022 0.0007 0.0003 0.0001 0.0000 0.0003 0.0002 0.0002 0.0001 0.0002 0.0002 0.0000 27 0.0006 0.0008 0.4605 0.3940 0.0942 0.0154 0.0209 0.0044 0.0047 0.0022 0.0007 0.0003 0.0001 0.0000 0.0003 0.0002 0.0002 0.0001 0.0002 0.0002 0.0000 28 0.0000 0.0004 0.1064 0.4622 0.2010 0.0360 0.0531 0.0198 0.0263 0.0293 0.0205 0.0178 0.0092 0.0039 0.0022 0.0030 0.0026 0.0039 0.0024 0.0000 0.0000 29 0.0000 0.0004 0.1064 0.4622 0.2010 0.0360 0.0531 0.0198 0.0263 0.0293 0.0205 0.0178 0.0092 0.0039 0.0022 0.0030 0.0026 0.0039 0.0024 0.0000 0.0000 30 0.0003 0.0008 0.3426 0.5261 0.1064 0.0103 0.0108 0.0012 0.0011 0.0002 0.0000 0.0000 0.0000 0.0000 0.0001 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 31 0.0003 0.0008 0.3426 0.5261 0.1064 0.0103 0.0108 0.0012 0.0011 0.0002 0.0000 0.0000 0.0000 0.0000 0.0001 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 34 0.0000 0.0000 0.0000 0.0243 0.5816 0.1466 0.2107 0.0203 0.0159 0.0001 0.0000 0.0000 0.0000 0.0000 0.0005 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 35 0.0000 0.0000 0.0000 0.0243 0.5816 0.1466 0.2107 0.0203 0.0159 0.0001 0.0000 0.0000 0.0000 0.0000 0.0005 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 36 0.0000 0.0000 0.0000 0.0000 0.0000 0.0003 0.0200 0.1776 0.2426 0.2220 0.1135 0.0786 0.0350 0.0131 0.0192 0.0218 0.0174 0.0218 0.0170 0.0000 0.0000 37 0.0000 0.0000 0.0000 0.0000 0.0000 0.0003 0.0200 0.1776 0.2426 0.2220 0.1135 0.0786 0.0350 0.0131 0.0192 0.0218 0.0174 0.0218 0.0170 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0003 0.0200 0.1776 0.2426 0.2220 0.1135 0.0786 0.0350 0.0131 0.0192 0.0218 0.0174 0.0218 0.0170 0.0000 0.0000 0.0000 0.0000 0.0000 0.0401 0.9589 0.0010 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 40 0.0000 0.0000 0.0000 0.0000 0.0010 0.3707 0.5348 0.0516 0.0403 0.0002 0.0000 0.0000 0.0000 0.0000 0.0014 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 41 0.0000 0.0000 0.0000 0.0000 0.0010 0.3707 0.5348 0.0516 0.0403 0.0002 0.0000 0.0000 0.0000 0.0000 0.0014 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 SP Butane 0.0000 0.0000 0.0000 0.0000 0.0010 0.3707 0.5348 0.0516 0.0403 0.0002 0.0000 0.0000 0.0000 0.0000 0.0014 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 32R 0.0003 0.0008 0.3424 0.5261 0.1064 0.0103 0.0108 0.0012 0.0011 0.0002 0.0000 0.0000 0.0000 0.0000 0.0001 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 32 0.0003 0.0008 0.3426 0.5261 0.1064 0.0103 0.0108 0.0012 0.0011 0.0002 0.0000 0.0000 0.0000 0.0000 0.0001 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 27R 0.0006 0.0008 0.4604 0.3941 0.0943 0.0154 0.0209 0.0044 0.0047 0.0022 0.0007 0.0003 0.0001 0.0000 0.0003 0.0002 0.0002 0.0001 0.0002 0.0002 0.0000 35R 0.0000 0.0000 0.0000 0.0243 0.5816 0.1466 0.2107 0.0203 0.0159 0.0001 0.0000 0.0000 0.0000 0.0000 0.0005 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 SP Condensate SP Propane ... Demethanizer C- 05 c máy ch Targeting ph tính ch c công c Column c l tháp C- 05 C? ?c n M s ên c – Mơ ph ình bày D sánh v t tính tốn, phân tích chi ti phân tích nhi -05 s 2.2 – Phân tích exergy M – Phân tích. .. thông s cho thi ,n tính ch c? ?ng c mơ ph sau òng v ành ph c -05 -05 v ã x? ?c c ho nhà máy ch %m thoát exergy cho tháp so v ình Li u Trang Lu cs ng d tháp C- 05 c a nhà máy ch bi n khí Dinh C u ki... cs ng d tháp C- 05 c a nhà máy ch bi n khí Dinh C u ki n v n hành t 2.2.2 Phân tích tháp C- 05 v 2.2 31 PHÂN TÍCH EXERGY .34 2.2.1 C? ?c m 34 2.2.2 C? ?n b 2.3 hi PHÂN TÍCH