《PRO Ⅱ化工软件工程应用》.doc

第1讲练习 ProII使用入门1.1建立以下过程的Pro/II模拟模型：将800 kmol/hr的低浓甲醇（甲醇20%w，水 80%w，20 C，1 bar）与1000 kmol/hr的高浓甲醇（甲醇 90%w，水10%w，30 C，1.5 bar）混合。求混合后的温度和体积流量。1.建立模型2.规定单位3.规定组分4.规定热力学模型5. 设定参数6. 运算结果Stream (Summary)UOMS3NameS3DescriptionS3PhaseLiquidThermodynamic SystemNRTL01Total Molar Ratekg-mol / hr1800Total Mass Ratekg / hr47295.99666TemperatureC25.6996957Pressurebar1Total Molecular Weight26.2755537Total Specific Enthalpykcal / kg18.13372114Total Cpkcal / kg C0.716938441Total Molar Component Rateskg-mol / hr H2O740.0000002 METHANOL1060Total Molar Component Fractionsfraction H2O0.411111111 METHANOL0.588888889Vapor Mole Fractionfraction0Vapor CompositionfractionVapor Component Ratekg-mol / hrTotal Liquid Molar Ratekg-mol / hr1800Total Liquid Mass Ratekg / hr47295.99666Total Liquid Molecular Weight26.2755537Total Liquid Mole Fractionfraction1Total Liquid Specific Enthalpykcal / kg18.13372114Total Liquid CPkcal / kg C0.716938441Total Liquid Compositionfraction H2O0.411111111 METHANOL0.588888889Total Liquid Component Ratekg-mol / hr H2O740.0000002 METHANOL1060Liquid CompositionfractionLiquid Component Ratekg-mol / hrLiquid1 CompositionfractionLiquid1 Component Ratekg-mol / hrLiquid2 CompositionfractionLiquid2 Component Ratekg-mol / hr第2讲练习 反应器的模拟2.1 甲烷与水蒸汽在镍催化剂下的转化反应为：原料气中甲烷与水蒸汽的摩尔比为1:4，流量为100 kmol/hr。若反应在恒压及等温条件下进行，系统总压为0.1013 MPa，温度为750 ，当反应器出口处CH4转化率为73%时，CO2和H2的产量是多少？反应热负荷是多少？ 反应和原料同示例conversion，若反应在恒压及绝热条件下进行，系统总压为0.1013 MPa，反应器进口温度为950 ，当反应器出口处CH4转化率为73%时，反应器出口温度是多少？ (Conversion Reactor)答2.11、连接物流2、设置单位3、选择组分4、选择热力学模型5、建立反应方程式6、输入物流7、输入转化率8运行并查看结果 THERMODYNAMIC SYSTEM SRK Molar Flowrates, KG-MOL/HRStream Physical PropertiesTotalVaporRate, KG-MOL/HR129.2000129.2000Temperature, C750.00750.00Pressure, MPA1.0130E-011.0130E-01Molecular Weight13.638413.6384Fraction 1.0000Enthalpy, KJ/KG-MOL45736.503445736.5034Cp, KJ/KG-C2.88022.8802CompNo.ComponentTotalVapor1METHANE5.40005.40002H2O50.800050.80003CO214.600014.60004H258.400058.4000Molar CompositionsCompNo.ComponentTotalVapor1METHANE0.04180.04182H2O0.39320.39323CO20.11300.11304H20.45200.45202.21、2、3、运行，导出结果Stream (Summary)UOMS2NameS2DescriptionS2PhaseVaporThermodynamic SystemSRK01Total Molar Ratekg-mol / hr129.2Total Mass Ratekg / hr1762.077599TemperatureC378.7391769PressureMPa0.1013Total Molecular Weight13.63837151Total Specific EnthalpykJ / kg2334.861232Total CpkJ / kg C2.608989526Total Molar Component Rateskg-mol / hr METHANE5.4 H2O50.8 CO214.6 H258.39999999Total Molar Component Fractionsfraction METHANE0.041795666 H2O0.393188855 CO20.113003096 H20.452012384Vapor Molar Ratekg-mol / hr129.2Vapor Mass Ratekg / hr1762.077599Vapor Molecular Weight13.63837151Vapor Mole Fractionfraction1Vapor Specific EnthalpykJ / kg2334.861232Vapor CPkJ / kg C2.608989526Vapor Compositionfraction METHANE0.041795666 H2O0.393188855 CO20.113003096 H20.452012384Vapor Component Ratekg-mol / hr METHANE5.4 H2O50.8 CO214.6 H258.39999999Total Liquid Molar Ratekg-mol / hr0Total Liquid Mass Ratekg / hr0Total Liquid Mole Fractionfraction0Total Liquid CompositionfractionTotal Liquid Component Ratekg-mol / hr第3讲练习 物性估算热力学模型的选择3.1 采用Pro/II计算在25时不同质量浓度甲醇水溶液（甲醇含量从0100%范围内变化）的密度，热力学计算方法选择NRTL模型。 答 1 画流程图2 规定单位3输入组分4热力学模型5输入物流6 规定反应器参数7.查看运行结果 NUMBER KG/M3 NUMBER KG/M3 Base 996.5125 1 999.0140 51 887.6061 2 996.5125 52 885.6309 3 994.0234 53 883.6644 4 991.5468 54 881.7066 5 989.0824 55 879.7575 6 986.6303 56 877.8169 7 984.1903 57 875.8849 8 981.7624 58 873.9614 9 979.3464 59 872.0463 10 976.9422 60 870.1396 11 974.5499 61 868.2413 12 972.1692 62 866.3512 13 969.8001 63 864.4692 14 967.4426 64 862.5955 15 965.0965 65 860.7299 16 962.7617 66 858.8723 17 960.4382 67 857.0227 18 958.1259 68 855.1810 19 955.8247 69 853.3473 20 953.5345 70 851.5214 21 951.2553 71 849.7033 22 948.9869 72 847.8930 23 946.7294 73 846.0903 24 944.4825 74 844.2953 25 942.2463 75 842.5079 26 940.0207 76 840.7281 27 937.8055 77 838.9557 28 935.6008 78 837.1908 29 933.4064 79 835.4333 30 931.2222 80 833.6832 31 929.0483 81 831.9404 32 926.8845 82 830.2049 33 924.7308 83 828.4766 34 922.5870 84 826.7555 35 920.4532 85 825.0415 36 918.3292 86 823.3346 37 916.2149 87 821.6348 38 914.1104 88 819.9419 39 912.0156 89 818.2560 40 909.9303 90 816.5771 41 907.8545 91 814.9050 42 905.7882 92 813.2398 43 903.7313 93 811.5813 44 901.6837 94 809.9296 45 899.6453 95 808.2846 46 897.6162 96 806.6463 47 895.5961 97 805.0146 48 893.5852 98 803.3894 49 891.5832 99 801.7709 50 889.5902 100 800.1588 101 798.5532第 38 页 共 38 页第4讲练习 分离单元的模拟4.1 对于含等摩尔的正戊烷和正己烷的溶液，试计算：(1)120下的露点压力;(2)1atm下的泡点温度;120,0.9atm时的气相分率,气相和液相中的摩尔分率。（闪蒸）答 1 画流程图2 规定单位3输入组分4热力学模型5输入物流6 规定反应器参数并且查看运行结果Temperature, F120.000Pressure, ATM0.759Pressure Drop, ATM0.241Mole Frac Vapor1.00000Mole Frac Liquid0.00000Mole Frac Mw Solid0.00000Duty, M*KCAL/HR0.00672FLASH TYPEDEW-T（2）Temperature, F119.907Pressure, ATM1.000Pressure Drop, ATM-1.000E-01Mole Frac Vapor0.00000Mole Frac Liquid1.00000Mole Frac Mw Solid0.00000Duty, M*KCAL/HR-0.00257FLASH TYPEBUBBLE-P(3）Temperature, F120.000Pressure, ATM0.900Pressure Drop, ATM0.000Mole Frac Vapor0.39364Mole Frac Liquid0.60636Mole Frac Mw Solid0.00000Duty, M*KCAL/HR0.00000FLASH TYPEISOTHERMALStream Physical PropertiesTotalVaporRate, KG-MOL/HR0.39360.3936Temperature, F120.00120.00Pressure, ATM9.0000E-019.0000E-01Molecular Weight76.978676.9786Fraction 1.0000Enthalpy, KCAL/KG-MOL8507.61448507.6144Cp, KCAL/KG-F0.23640.2364Molar Flowrates, KG-MOL/HRCompNo.ComponentTotalVapor1PENTANE0.25810.25812HEXANE0.13550.1355Molar CompositionsCompNo.ComponentTotalVapor1PENTANE0.65580.65582HEXANE0.34420.3442Stream Physical PropertiesTotalLiquidRate, KG-MOL/HR0.60640.6064Temperature, F120.00120.00Pressure, ATM9.0000E-019.0000E-01Molecular Weight80.582280.5822Fraction 1.0000Enthalpy, KCAL/KG-MOL2055.66202055.6620Cp, KCAL/KG-F0.31690.3169Molar Flowrates, KG-MOL/HRCompNo.ComponentTotalLiquid1PENTANE0.24190.24192HEXANE0.36450.3645Molar CompositionsCompNo.ComponentTotalLiquid1PENTANE0.39890.39892HEXANE0.60110.60114.2 要求用一个精馏塔分离苯和苯乙烯在77和1atm条件下的等摩尔混合物。塔顶馏出物中苯含量应当为99mol%，且应包含进塔原料中95mol%的苯。（1）用过程模拟软件确定全回流下的最少理论塔板数（Nmin）、最小回流比（Rmin）和R1.3 Rmin时处于平衡的理论塔板数。（2）根据（1）确定的理论板数和回流比对该精馏塔进行核算，求出精馏塔的冷凝器热负荷和再沸器热负荷。（精馏）答 (1)1 画工艺流程2 选择单位3选择组分4热力学模型5输入参数6规定产品要求7运行并查看结果SPECIFICATIONS PARAMETER COMP. SPECIFICATION SPECIFIED CALCULATED TYPE NUM TYPE VALUE VALUE - - - - - STRM S2 1 MOL FRACTION 9.900E-01 9.881E-01 STRM S2 1 MOL RATIO 9.500E-01 9.482E-01 SUMMARY OF UNDERWOOD CALCULATIONS MINIMUM REFLUX RATIO 0.22281 FEED CONDITION Q 1.36451 FENSKE MINIMUM TRAYS 3.95963 OPERATING REFLUX RATIO 1.30 * R-MINIMUM TOTAL FEED R/R-MIN M/M-MIN REFLUX DUTY, M*KCAL/HR TRAYS TRAY RATIO CONDENSER REBOILER - - - - - - - 13 9.03 1.150 3.328 0.256 -4.471E-01 8.133E-01 12 8.13 1.225 2.974 0.273 -4.531E-01 8.192E-01 11 7.47 1.300 2.718 0.290 -4.590E-01 8.252E-01 10 7.28 1.375 2.643 0.306 -4.649E-01 8.311E-01 10 7.10 1.450 2.574 0.323 -4.709E-01 8.371E-01 (1) NORMAL VAPOR VOLUME IS 22.414 M3/KG-MOLE (0 C AND 1 ATM)答 (2)1 画工艺流程2 选择单位3选择组分4热力学模型5输入参数6规定产品要求7运行并查看结果Column SummaryNet Flow RatesTrayTemperature FPressureATMLiquidVaporFeedProductHeater DutiesM*KCAL/HRKG-MOL/HR1C176.81.0016.0 48.0L-0.47352180.31.0015.263.9 3185.91.0014.363.2 4192.31.0013.662.3 5197.61.0013.261.6 6201.01.0012.961.2 7202.91.00149.560.9100.0L 8208.31.00146.597.5 9223.71.00141.594.5 10251.91.00139.889.4 11R278.51.00 87.8 52.0L0.8404 第5讲 换热器、压力改变单元的模拟5.1 在由氯气和乙烯生产氯乙烯的过程中，从高温裂解炉出口的物流中含有58300 lb/h的HCl，100000 lb/h的氯乙烯，105500 lb/h的1,2-二氯乙烷，温度为500，压力为26atm。在进入精馏工序之前，要通过冷却和冷凝使该物流温度降至6，压力降至12atm。设该过程以三步完成：（1）26atm下在换热器1中冷却至露点温度；（2）经由一阀门绝热膨胀到12atm；（3）12atm下在换热器2中冷却至6。试确定每个换热器的热负荷。（换热器）答 :1 画工艺流程2 选择单位3选择组分4热力学模型5输入参数6规定产品要求7运行并查看结果 UNIT 1, E1 OPERATING CONDITIONS DUTY, M*KCAL/HR 11.772 HOT SIDE CONDITIONS INLET OUTLET FEED S1 VAPOR PRODUCT S2 VAPOR, LB-MOL/HR 4265.119 4265.119 K*LB/HR 263.800 263.800 CP, KCAL/LB-C 0.140 0.124 TOTAL, LB-MOL/HR 4265.119 4265.119 K*LB/HR 263.800 263.800 CONDENSATION, LB-MOL/HR 0.000 TEMPERATURE, C 500.000 156.505 PRESSURE, ATM 26.000 26.000 UNIT 2, E2 OPERATING CONDITIONS DUTY, M*KCAL/HR 13.190 HOT SIDE CONDITIONS INLET OUTLET FEED S3 LIQUID PRODUCT S4 VAPOR, LB-MOL/HR 4265.119 K*LB/HR 263.800 CP, KCAL/LB-C 0.111 LIQUID, LB-MOL/HR 4265.119 K*LB/HR 263.800 CP, KCAL/LB-C 0.154 TOTAL, LB-MOL/HR 4265.119 4265.119 K*LB/HR 263.800 263.800 CONDENSATION, LB-MOL/HR 4265.119 TEMPERATURE, C 139.176 6.000 PRESSURE, ATM 12.000 12.0005.2 一压缩机将压强为 1.1 bar 的空气加压到 3.3 bar，空气的温度为 25 C，流量为 1000 m3/h。压缩机的多变效率为 0.71，驱动机构的机械效率为 0.97。求：压缩机所需要的轴功率、驱动机的功率以及空气的出口温度和体积流量各是多少？（压缩机）答 :1 画工艺流程2 选择单位3选择组分4热力学模型5输入参数6规定产品要求7运行并查看