化学化工学院 课程设计说明书
V1?2956.98Nm3
其中 CH4 V1,CH4?2956.98?0.011?32.527Nm3
Ar V1,Ar?2956.98?0.0033?9.758Nm3 H2 V1,H2?2956.98?0.7445?2201.472Nm3 N2 V1,N2?2956.98?0.2412?713.223Nm3
2956.9?8进器气体物料 V18?V1?V17?8948.?69111N93m0 5.671进器气体组分含量 V1i8?,V?i1,V
i其中 NH3 V18,NH3? V17,NH3?580.769Nm3
?7CH4 V18CH,4?32.521305?.64131Nm33 8.168Ar V18,Ar?9.758?394.739?404.497Nm3
72H2 V18H,2?2201.4?3499?9.948N7m2 01.42?31667?.594N2 V18N,2?713.2232N3m8 0.817各组分百分含量 y1i8?,V1i8,V18
NH3 y18NH,3?580.769?100%?11905.6714.87 8%CH4 y18,CH4?1338.168?100%?11.239%
11905.671Ar y18,Ar?404.497?100%?3.398%
11905.6717201.42?100%?60.487%
11905.6712380.817?100%?19.998%
11905.671H2 y18,H2?N2 y18,N2?进器液体等于冷交换器冷凝液氨量 L18?L18,NH3?L17,NH3?284.979Nm3
36 化学化工学院 课程设计说明书
进器总物料＝V18?L18?11905.671?284.979?12190.650Nm3
出器物料：已知出器气体中氨含量为 2.5%，设出器气体中氨含量为bNm3。
b4.8783 解得 b?290.38 N2m?11905.671?580.7690.025则氨冷器中冷凝液氨量： L?18,NH3?V18,NH3?b?580.769?290.382?290.387Nm3
??L?L氨冷器出器总液氨量: L2N,H18N,H331N83,H?284.97?9290.?3875N73m5 .36611905.67?1氨冷器出器气量: V2?V18?b?290?.382311N6m15.289
其中 NH3 V2,NH3?290.382Nm3
CH4 V2,CH4?V18,CH4?1338.168Nm3 Ar V2,Ar? V18,Ar?404.497Nm3 H2 V2,H2?V18,H2?7201.42Nm3 N2 V2,N2?V18,N2?2380817Nm3
各组分百分含量 y2,i?V2,iV2
NH3 y2,NH?3290.382?100%?2.499%
11615.2891338.168?100%?11.521%
11615.289CH4 y2,CH?4Ar y2,Ar?404.497?100%?3.482%
11615.2897201.42?100%?61.999%
11615.2892380.817?100%?20.498%
11615.289H2 y2,H?2N2 y2,N?2出器总物料?V2?L2,NH3?11615.289?575.366?12190.655Nm3
37 化学化工学院 课程设计说明书
4.1.16 冷交换器物料计算： 图4-1-4 冷交换器物料计算示意图
V17 V2 V14 V3 进口物料：冷交换器进口总物料等于氨冷器出口总物料
38m9； 其中气体入口xNH3?0.98425 V2?11615.2N液体入口
LNH3?575.366Nm3；
由气液平衡计算得，以 1kmol进口物料为计算基准：即 F?1
6 .1L?V?F ?4.1.1?L?xNH3?V?yNH3?F?mNH3 ?4.1.16.2?
将 yNH3?0.025 ，xNH3?0.98425代入上式：
V?xNH3?mNH3xNH?yNH33?1.026?mNH30.95925 ?4.1.16? .3V2,NH3V2?4.1.16.3?式中
mNH3 可由物料平衡和氨平衡计算 mNH3?
?V2??V1?V17 ?4.1.16.4? ?V17?V18?V13?L15 ?4.1.16? .5?V2,NH?V2,NH3?L17,NH3?L?18,NH3 ?4.1.16? .63?式中 V2?—冷交换器入口总物料； V17—冷交换器热气出口总物料 ? V2,NH3—冷交换器入口总氨物料
将 V8?10212.836Nm3，V13?135.479Nm3，L15?843.687Nm3 代入上式解得：
V?17?9233.67Nm3
∴ V2??2956.98?9233.67?12190.65Nm3；
?3V2,NH3?284.979?290.387?290.382?865.748Nm
38 化学化工学院 课程设计说明书
?V2,NH3∴ mNH3?V2??865.748.3 ?0.071017代入 ?4.1.16?得：
9233.67V?1.026?0.071017?0.95197; L?1?V?0.04803;
0.95925L0.04803??0.05045 V0.95197由
LLL 可求出冷交换器冷凝液体量 16??0.05045
V3VV冷凝液体量 L16?0.05045V3?0.05045?11607.77?585.612Nm3
出器物料：冷交换器（冷气）出口气体物料等于进口总物料减去冷凝液体量。
V3?12190.65?585.612?11605.038Nm3
其中 NH3 V3,NH3?11605.038?2.5%?290.126Nm3
CH4 V3,CH4?11605.038?11.539%?1339.105Nm3 Ar V3,Ar?11605.038?3.462%?401.766Nm3 H2 V3,H2?11605.038?61.874%?7180.501Nm3 N2 V3,N2?11605.038?20.625%?2393.539Nm3
计算误差?V3?V511605.038?11607.77?100%??100%??0.0235% V511607.77校核氨分离器液氨百分数 氨分离器液氨百分数：
G分%??L15?x15?100%L15?L16?x16843.687?0.95618?100%?58.325?3.687?0.95618?585.612?0.98425
冷交换器分离液氨百分数：G冷%?1?G分%?1?58.325%?41.675% 计算误差?G??G分0.57554?0.58325??100%??1.322％ G分0.58325 39 化学化工学院 课程设计说明书
4.1.17液氨贮槽物料计算:
进槽物料：氨分离器入槽液体 L15?843.687Nm3
87 其中 NH3 L15NH,3?843.6?0.9?5618Nm8036 .667 CH4 L15,CH4?843.687?0.01731?14.623Nm3 Ar L15,Ar?843.687?0.00157?1.330Nm3
?7 H2 L15H,2?843.68?7N2 L15N,?2843.6830.01?973N1m6 .56630.00?521Nm4 .501冷交换器入槽液体 L16?585.612Nm3
120.9?8425 其中 NH3 L16NH,3?585.6x12 CH4 L16CH,4?585.6?Nm5736 .38930.0?0427Nm2 .501Ar L16,Ar? 585.612?0.00068?0.398Nm3 H2 L16,H2? 585.612?0.00825?4.831Nm3 N2 L16,N2? 585.612?0.00255?1.493Nm3
入槽混合物料 L21?L15?L16?843.687?585.612?1429.299Nm3 各组分物料含量： L21,i?L15,i?L16,i
67 其中 NH3 L21NH,3?806.6?576?.38931Nm383.056
CH4 L21,CH4?14.623?2.501?17.124Nm3
Ar L21,Ar?1.33?0.398?1.728Nm3 H2 L21,H2?16.566?4.831?21.397Nm3
11.4?93N2 L21N,2?4.50?35N.m9 94L21i,百分含量 x21i,?
L21 40