case_02吸收稳定系统流程模拟案例.doc

分离工程工业应用实例：催化裂化吸收稳定系统模拟1 工艺和计算用的流程简述催化裂化装置是主要的炼油装置之一。它是将重质油轻质化，生产液化气、汽油和柴油的重要装置。而吸收稳定装置是催化裂化装置中的后处理系统，它将来自催化分馏塔塔顶的原料粗汽油和富气分离成产品液化气和稳定汽油，同时得到副产品干气。本算例是以某石化公司的吸收稳定系统实际装置为例，详细阐述了其流程及算法。催化裂化吸收稳定系统双塔流程共有四个塔，即：吸收塔、解吸塔、再吸收塔和稳定塔。此外，还有两个油气分离罐，即：压缩机后汽液分离罐和稳定塔塔顶回流罐。工艺流程如下：补充吸收剂（稳定汽油）进入吸收塔的顶部，粗汽油作为吸收剂进入吸收塔的上部。吸收塔设有3个中段取热，以取走吸收过程中放出的热量。吸收塔顶部引出的贫气直接进入再吸收塔的底部，吸收塔底的饱和吸收油与压缩富气和解吸塔解吸气混合冷却后进入汽液分离罐。汽液分离罐的气相进入吸收塔的底部，液相经泵加压后进入解吸塔的上部，解吸塔由塔底再沸器提供热量。稳定塔塔底脱乙烷汽油先与稳定汽油换热，再进入稳定塔的中部，经稳定塔分出稳定汽油和液化气。轻柴油作为再吸收塔的吸收油进入再吸收塔的顶部，吸收贫气中夹带的重组分。干气从再吸收塔顶放出并入瓦斯管网，富吸收油返回分馏塔。工艺流程如图1-1所示：图1-1 催化裂化吸收稳定系统工艺流程图图例说明：1 富气 2 粗汽油 3 轻柴油 4 压缩机 5 汽液平衡罐前冷却器 6 汽液平衡罐 7 平衡罐气相 8 平衡罐液相 9 补充吸收剂提压泵 10 吸收塔 11 解吸塔 12 补充吸收剂 13 稳定汽油产品 14 换热器 15 吸收塔中间冷却器 16 贫气 17 脱乙烷汽油 18 稳定汽油 19 再吸收塔 20 干气 21 富吸收油 22 稳定塔 23 液化气2 需要输入的主要参数原料、主要设备操作参数如 表2-1、表2-2所示。表2-1 原料组成富气粗汽油轻柴油温度/404040压力/MPa0.171.61.5流量/(kMol/h)188.0000136.675088.5组分流量/(kMol/h)H2O0.00000.00001.1948H2S0.00000.00000.0000空气0.00000.00000.0000H213.42700.00000.0000023.18850.00000.0000N217.30920.00000.0000CO0.23880.00000.0000CO21.33860.00000.0000甲烷12.36850.00000.0000乙烷4.56840.00000.0000乙烯10.40020.00000.0000丙烷5.47272.97580.0000丙烯42.33010.00000.0000异丁烷22.25920.00000.0000正丁烷5.700212.12360.00001-丁烯20.576622.42670.0000异丁烯0.00000.00000.0000顺-2-丁烯8.86980.00000.0000反-2-丁烯5.56290.00000.0000正戊烷14.389512.82290.0170异戊烷0.00000.00000.0000环戊烷0.00001.75270.00001-戊烯0.000026.49570.02241-己烯0.000011.78760.0867环己烷0.00001.48140.0344正己烷0.00007.27020.0658苯0.00001.31870.02701,3-己炔0.00000.00000.0000环庚烷0.00001.55480.4670正庚烷0.00002.61560.1137甲苯0.00004.96400.5907正辛烷0.00002.11750.8472环辛烷0.00001.22153.53121-辛烯0.00000.60110.1381苯乙烷0.00007.873419.1160正壬烷0.00000.86581.59301-甲基-2-乙基苯0.00000.48065.1950正癸烷0.00000.52640.7114丁苯0.00006.609913.7441十一烷烃0.00000.22121.0974戊苯0.00003.55492.25681-庚烯0.00002.54740.07791-甲基-3-乙基苯0.00000.465337.5577表2-2主要设备操作参数序号设备操作参数1富气压缩机机后压力1.5MPa，等熵效率80%2汽液平衡罐压力1.47MPa，温度403补充吸收剂提压泵泵后压力1.5MPa4稳定塔进料热交换器冷热流体出口温差55吸收塔中间冷却器冷却水温度30，热流体返塔温度336稳定汽油冷却器热流体出口温度357吸收塔塔顶压力1.43MPa，全塔压降0.03MPa；全塔理论级数28；粗汽油进第3块理论板，补充吸收剂进第1块理论板，汽液平衡罐气相进第28块理论板；8解吸塔塔顶压力1.46MPa，全塔压降0.02MPa；全塔理论级数28；汽液平衡罐液相进第1块理论板，补充吸收剂进第一块理论板；9再吸收塔塔顶压力1.37MPa，全塔压降0.03MPa；全塔理论级数16；贫气进第16块理论板，轻柴油进第1块理论板；10稳定塔塔顶压力1.37MPa，全塔压降0.03MPa；全塔理论级数35；稳定汽油进第16块理论板；塔顶冷凝器压力0.85MPa；3.软件版本采用PRO/软件6.0版。4.结果分析输入数据迭代收敛后，在满足解吸塔塔底脱乙烷汽油、液化气、稳定汽油产品质量的前提下，逐步调整补充吸收剂的流量，使得贫气中的C3含量满足产品质量指标。表4-1产品质量控制指标序号产品控制指标1贫气C31.5%（v%）2解吸塔塔底脱乙烷汽油C20.2%（M%）3液化气C50.8%（M%）4稳定汽油C41.0%（M%）5. 输入文件TITLE PROJECT=20080319, PROBLEM=XIWEN, USER=LGT, DATE=03/19/2008 DBASE DATA=PC1 PRINT INPUT=ALL, STREAM=ALL, RATE=WT, FRACTION=M, TBP TOLERANCE PRESSURE=0.001, TEMPERATURE=-0.01, DUTY=0.0001, & MISCELLANEOUS=0.0003, STREAM=0.001,-0.4,0.001 DIMENSION METRIC, TEMP=C, PRES=MPA, WT=KG, TIME=HR, LIQVOL=M3, & VAPVOL=M3, XDENSITY=SPGR, ENERGY=KJ, WORK=KW, CONDUCT=KCH, & VISCOSITY=CP, SURFACE=DYNE SEQUENCE SIMSCI CALCULATION TRIALS=200, RECYCLE=ALL, COMPCHECK=CALC, DVARIABLE=ON, & FLASH=DEFAULT, MAXOPS=50000, CDATA=FIX EXERGY TZERO=30, PZERO=0.10132COMPONENT DATA LIBID 1,H20/2,H2S/3,AIR/4,H2/5,O2/6,N2/7,CO/8,CO2/9,METHANE,CH4/ & 10,ETHANE,C2H6/11,ETLN,C2H4/12,PROPANE,C3H8/13,PRLN,C3H6/ & 14,IC4,YIC4H10/15,BUTANE,ZHENGC4H10/16,BUT1,1-C4H8/ & 17,IBTE,YIC4H8/18,C2BUTENE,SHUN-2-C4H8/ & 19,T2BUTENE,FAN-2-C4H8/20,C5H12/21,IPENTANE,YIC5H12/ & 22,CYPNTANE,HUANC5H10/23,1PENTENE,C5H10XI/ & 24,1HEXENE,1-C6H12/25,CH,HUANC6H12/26,C6H14/27,C6H6/ & 28,12BD,1-2-C6H10/29,CHP,HUANC7H14/30,HEPTANE,C7H16/ & 31,TOLUENE,JIABENC7/32,OCTANE,C8H18/33,COCT,HUANC8H16/ & 34,1OCTENE,XI-1-C8H16/35,EBENZENE,BENYIWANC8H10/ & 36,NONANE,C9H20/37,M2EZ,YIWANJIABENC9/38,DECANE,C10H22/ & 39,BBENZENE,DINGBENC10/40,NC11,C11H24/41,PNBZ,WUBENC11/ & 42,1HEPTENE,1-C7H14-XI/43,M3EZ,M-YIWANJIABEN-C9, & BANK=PROCESS,SIMSCI,OLILIB CUTPOINTS TBPCUTS=20,205,20/360,20/500,10,DEFAULTTHERMODYNAMIC DATA METHOD KVAL(VLE)=SRK, VISCOSITY(L)=PETR, VISCOSITY(V)=PETR, & CONDUCTIVITY(L)=PETR, CONDUCTIVITY(V)=PETR, SURFTENSION=PETR, & ENTHALPY(L)=SRK, ENTHALPY(V)=SRK, DENSITY(L)=API, & DENSITY(V)=SRK, ENTROPY(L)=SRK, ENTROPY(V)=SRK, SET=SET01, & DEFAULT WATER DECANT=OFFSTREAM DATA PROPERTY STREAM=FQ, TEMPERATURE=40, PRESSURE=0.17, PHASE=M, & RATE(M)=188, COMPOSITION(M)=4,7.142/5,1.696/6,9.207/7,0.127/ & 8,0.712/9,6.579/10,2.43/11,5.532/12,2.911/13,22.516/14,11.84/ & 15,3.032/16,10.945/18,4.718/19,2.959/20,7.654, NORMALIZE PROPERTY STREAM=ZQY, TEMPERATURE=40, PRESSURE=1.6, PHASE=M, & RATE(WT)=4000, COMPOSITION(M)=12,0.81/15,2.2/16,4.01/20,3.07/ & 22,0.67/23,7.24/24,6.7/25,0.94/26,3.6/27,0.92/29,1.74/30,2.81/ & 31,6.8/32,3.72/33,2.81/34,1.02/35,15.94/36,2.27/37,1.26/ & 38,1.38/39,16.55/40,0.58/41,9.32/42,1.95/43,1.22, NORMALIZE PROPERTY STREAM=QCY, TEMPERATURE=40, PRESSURE=1.45, PHASE=M, & RATE(M)=88.4999, COMPOSITION(M)=1,0.0135/10,2.3928E-9/ & 11,1.3702E-9/12,1.6355E-7/13,6.8189E-7/14,5.7355E-6/ & 15,7.2028E-6/16,9.0218E-6/17,4.3181E-6/18,6.7383E-6/ & 19,6.1637E-6/20,0.00019167/22,7.4874E-5/23,0.0002535/ & 24,0.00097941/25,0.00038895/26,0.000744/27,0.00030555/ & 28,5.138E-5/29,0.0052773/30,0.001285/31,0.0066743/ & 32,0.0095726/33,0.0399/34,0.0015606/35,0.216/36,0.018/ & 37,0.0587/38,0.0080382/39,0.1553/40,0.0124/41,0.0255/ & 42,0.00088038/43,0.42438, NORMALIZE PROPERTY STREAM=QQY, TEMPERATURE=40, PRESSURE=1.6, PHASE=M, & RATE(WT)=6999.98, COMPOSITION(WT)=12,1.68/15,9.37/16,16.75/ & 20,12.01/22,1.5/23,23.78/24,11.1/25,1.35/26,7.26/27,1.08/ & 29,1.25/30,2.21/31,3.12/32,1.14/33,0.24/34,0.34/35,2.72/ & 39,0.57/42,2.53, NORMALIZE PROPERTY STREAM=S10, REFSTREAM=ZQY PROPERTY STREAM=S11, REFSTREAM=QQYUNIT OPERATIONS MIXER UID=M1 FEED S10,S11 PRODUCT M=S9 COMPRESSOR UID=C1 FEED FQ PRODUCT M=S1 OPERATION CALCULATION=ASME, PRES=1.5 HX UID=E1 HOT FEED=S4, M=S5 OPER HTEMP=40 FLASH UID=F1 FEED S5 PRODUCT V=F2V, L=S6 ADIABATIC PRESSURE=1.47 HX UID=E3 HOT FEED=303C, M=S7 COLD FEED=S6, M=S2 CONFIGURE COUNTER OPER CTEMP=60 HX UID=E2 HOT FEED=S7, M=303E OPER HTEMP=35 SPLITTER UID=FL3 FEED 303E PRODUCT M=BX, M=S8 OPERATION PRESSURE=1.2, OPTION=FILL SPEC STREAM=BX, RATE(KGM/H),TOTAL,WET, VALUE=90 PUMP UID=P1 FEED BX PRODUCT M=S3 OPERATION PRESSURE=1.5 COLUMN UID=T301 PARAMETER TRAY=28,IO=1000 FEED F2V,28/ZQY,3/QQY,3/S3,1 PRODUCT OVHD(M)=301A, BTMS(M)=301B,259, SUPERSEDE=ON DUTY 1,4,1/2,12,2/3,23,3 PA NAME=1, FROM=3, TO=4, PHASE=L, PRES=1.5, TEMP=33 PA NAME=2, FROM=11, TO=12, PHASE=L, TEMP=33 PA NAME=3, FROM=22, TO=23, PHASE=L, TEMP=33 PSPEC PTOP=1.43, DPCOLUMN=0.03 PRINT PROPTABLE=PART ESTIMATE MODEL=CONVENTIONAL, TTEMP=42, BTEMP=48 TEMPERATURE 1,42/11,48 SPEC TRAY=3, RATE(WT,KG/H), PHASE=L,WET, VALUE=50 SPEC TRAY=11, RATE(WT,KG/H), PHASE=L,WET, VALUE=50 SPEC TRAY=22, RATE(WT,KG/H), PHASE=L,WET, VALUE=50 VARY DUTY=1,2,3 COLUMN UID=T302 PARAMETER TRAY=28,IO=60 DAMPING=0.9 FEED S2,1 PRODUCT OVHD(M)=302A,69.9998, BTMS(M)=302B, SUPERSEDE=ON DUTY 1,28,REBOILER PSPEC PTOP=1.46, DPCOLUMN=0.02 PRINT PROPTABLE=PART ESTIMATE MODEL=SIMPLE, TTEMP=85, RTEMP=140 TEMPERATURE 1,85/8,140 SPEC STREAM=302B,FRACTION, COMP=10,11,WET, VALUE=0.002 VARY DUTY=1 REBOILER TYPE=KETTLE MIXER UID=MIX FEED 301B,302A,S1 PRODUCT M=S4 HX UID=HX4 HOT FEED=303B, L=303C COLD FEED=302B, L=302C CONFIGURE COUNTER OPER HOCO=5 COLUMN UID=T303 PARAMETER TRAY=35,IO=60 DAMPING=0.9 FEED 302C,16 PRODUCT OVHD(M)=303A,100, BTMS(M)=303B, SUPERSEDE=ON CONDENSER TYPE=BUBB, PRESSURE=0.85, TEST=60 DUTY 1,1,CONDENSER/2,35,REBOILER PSPEC PTOP=1.37, DPCOLUMN=0.03 P