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Ar =11607.770×3.357%=389.673m3 H2 =11607.770×61.874%=7182.692m3 N2 =11607.770×20.625%=2394.103m3
合成塔一出，二进物料，热交换器，冷气进出物料等于合成塔入塔物料 即：V5=V6=V7=11607.770 m3 出塔物料：V8=10212.836m3
NH3 =10212.836×16.5%=1685.118m3 CH4 =10212.836×13.223%=1350.443m3 Ar =10212.836×3.816%=389.722m3 H2 =10212.836×49.838%=5089.873m3 N2 =10212.836×16.612%=1696.563m3 合成塔生成氨含量：
=1685.118－290.194=1394.924 m3
废热锅炉进出口物料，热交换器进出口物料等于合成塔出塔的物料。 即V8=V9=V10=10212.836 m3 3.3.10 水冷器物料计算
进器物料：水冷器进气物料等于热交换器出口物料，即V10入=10212.836m3 出器物料：在水冷器中部分氨气被冷凝；由氨分离器气液平衡计算得气液比 (V÷L)=11.110,有如下方程：
==11.110
（3-6）
V11出+L11出=L10入=10212.836 （3-7）
将V11出=11.110L11出带入（3-7）得：
L11出=843.687m3 V11出=9369.149m3
出口气体组分由V11i=V11出×y11i得:
其中：NH3 =9369.149×9.376%=878.451m3
CH4 =9369.149×14.269%=1336.884m3 Ar =9369.149×4.145%=388.351m3 H2 =9369.149×54.148%=5073.307m3 N2 =9369.149×18.061%=1692.062m3
出口液体各组分由L11i=V8i－V11i
其中：NH3 =1685.118－878.451=806.667m3 CH4 =1350.443－1336.884=13.559m3
Ar =389.722－388.351=1.371m3 H2 =5089.873－5073.307=16.566m3 N2 =1696.563－1692.062=4.501m3
3.3.11氨分离器物料计算
进器物料：氨分离器进器总物料等于水冷器出口气液混合物总物料 即V11=V11出+L11出=9369.149+843.687=10212.836 m3
出器物料：气液混合物在器内进行分离，分别得到气体和液体 出器气体V12＝V11出＝9369.149m3 出器液体 L15＝L11出＝843.687m3 氨分离器出口气体放空V13=135.479m3 其中：NH3 =135.479×9.376%=12.703m3 CH4 =135.479×14.269%=19.331m3
Ar =135.479×4.145%=5.616m3
H2 =135.479×54.148%=73.359m3
N2 =135.479×18.061%=24.469m3
3.3.12 冷交换器物料计算
进器物料：进器物料等于氨分离器出口气体物料减去放空气量 V14=V12－V13=9369.149－135.479=9233.670 m3 其中：NH3 =9233.670×9.376%=865.749m3
CH4 =9233.670×14.269%=1317.552m3 Ar =9233.670×4.145%=382.736m3 H2 =9233.670×54.148%=4999.849m3 N2 =9233.670×18.061%=1667.693m3 出器物料（热气）： 设热气出口温度T=17℃
查 T=17℃(由热量计算核定），p=28.42MPa气相平衡氨含量=5.9%，计算热气出口冷凝液氨时，忽略溶解在液氨中的气体。取过饱和度10% 故=1.1×5.9%=6.49% 设热气出口氨体积为a，则：
a?6.49%
9233.67?865.749?a计算得a=580.769
865.749－580.769=284.980m3 冷交换器热气出口气量及组分： 其中：NH3 =580.769m3 CH4 =1317.552m3
Ar =382.736m3
H2 =4999.849m3
N2 =1667.693m3
出口总气量 =9233.670－284.980=8948.690 m3 出口气体各组分：
NH3 =580.769÷8948.690×100%=6.490% CH4 =1317.522÷8948.690×100%=14.723% Ar =382.736÷8948.690×100%=4.277% H2 =4999.849÷8948.690×100%=55.872% N2 =1667.693÷8948.690×100%=18.636%
3.3.13 氨冷器的物料计算
进器物料：氨冷器进器物料等于冷交换器出器物料加上补充新鲜气物料V1=2956.387m3
其中：CH4 =2956.387×0.0111=32.816m3 Ar =2956.387×0.0032=9.460m3
H2 =2956.387×0.7475=2201.030m3 N2 =2956.387×0.2412=712.785m3
V18（进器气体物料）=V1+V17=2956.387+8948.691=11905.078m3 进器气体组分含量V18i=V1i+V17i 其中：NH3 580.769m3
CH4 = 32.816+1317.552=1350.368m3
Ar =9.460+382.736=392.196m3 H2 = 2201.030+4999.849=7200.879m3 N2 = 712.785+1667.693=2380.478m3
各组分百分含量：
NH3
=580.769÷11905.078×100%=4.878%
CH4 =1350.368÷11905.078×100%=11.343% Ar =392.196÷11905.078×100%=3.294% H2 =7200.879÷11905.078×100%=60.486%3 N2 =2380.478÷11905.078×100%=19.995%
进器液体等于冷交换器冷凝液氨量： =284.980 m3
进器总物料＝V18+L18=11905.078+284.980=12190.058 m3
出器Ⅰ物料：已知出器Ⅰ气体中氨含量为4.411%，出器II气体中氨含量2.5%，设出器气体中氨含量为bⅠ m3
bI4.411?
11905.078?580.769?bI2.5解得 bⅠ=290.382m3 则氨冷器中冷凝液氨量： =580.769－290.382=290.387m3
氨冷器出口总液氨量： 284.980+290.387=575.367m3 氨冷器出口气量：
V2=V18－b=11905.078－290.387=11614.691 m3 其中：NH3 = 290.382m3 CH4 = =1350.368m3
Ar = =392.196m3 H2 = =7200.879m3 N2 = =2380.478m3
各组分百分含量：
NH3 =290.382÷11614.691×100%=2.501% CH4 =1350.368÷11614.691×100%=11.626%