液平衡计算：查t15℃p13062MPa的平衡常数KNH3002522KCH474585KAr72752KH213332KN2693699
冷交换器出口液体组分含量：出口液体甲烷含量xCH4yCH4KCH401113674585x100％0149％出口液体氨含量xNH3yNH3KNH30025002522x100％99110％出口液体氩含量xAryArKAr00386472725x100％0053％出口液体氢含量xH2yH2KH206187513332x100％0464％出口液体氮含量xN2yN2KN202062593966x100％0149％冷交换器出口液体组分含量（％）NH399110CH40149Ar0053H20464N20149小计10000
136液氨贮槽气液平衡计算：由于氨分离器液体和冷交换器出口分离液体汇合后进入液氨贮槽经减压后溶解在液氨中的气体会解吸，即弛放气两种液体百分比估算值，即水冷后分离液氨占总量的白分数G％（1y5NH3）xy8NH3yNH3分y8NH3y5NH3x1yNH3分10025）x（0165013741）（01650025）x（1013741）x100％23418％水冷后分离液氨占总量的23418％冷交，氨冷后分离液氨占总量的76582％液氨贮槽入口1Kmol液体计算为准，即L01Kmol，入口液体混合后组分含量：m0iL15xX15iL16xX16iG％xL0xX15i1G％xX16i023418xX15i076582X16i混合后入口氨含量：m0NH3023418x09848076582x09911098962混合后入口甲烷含量m0CH4023418x00057076582x0001490002476混合后入口氩含量m0Ar023418x00070076582x000053000057混合后入口氢含量：m0H2023418x00064076582x0004640005052混合后入口氮含量：m0N2023418x00024076582x0002240002277液氨贮槽入口液体含量m0NH3098962KNH30598m0CH40002476KCH4170m0Ar000057m0H20005052KAr540m0N20002277KH2575小计10000KN2620
当热t17℃平衡计算得，平衡常数P1568MPa
根据气液平衡Lim0i1VLxki设VL00275代入上式得出口液体氨含量：LNH3m0NH31VLxkNH30989100275x05980972999Kmol出口液体甲烷含量：LCH4m0CH41VLxkCH40002476100275x1700000436Kmol
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f化工课程设计
出口液体氩含量：LArm0Ar1VLxkAr000057100275x5400000036Kmol出口液体氢气含量：LH2m0H21VLxkH20005052100275x5750003Kmol出口液体氮气含量：LN2m0N21VLxkN20002277100275x6200000126KmolL总0973897V109738970026103KmolVL＇VL00268误差0275002680027524％当VL0025时LNH30974432KmolLCH40000472KmolLAr0000039KmolLH20000328KmolLN20000138KmolV1L总0024591VL＇VL0024591097540900251误差0025002520025x100％04％出口液体组分含量：出口液体氨含量：xNH3LNH3L09744320975409x100％998998％出口r