河南城建学院毕业论文（设计）
V出=1583.47307m3(标)
3.3.8 合成塔物料计算
入塔物料：V5=17075.67272 m3(标)
其中 NH3 V5 NH3 = 17075.67272 ? 0.02=341.51345m3(标) CH4 V5CH4 =17075.67272 ? 0.11719=2001.09809m3(标) Ar V5AR =17075.67272 ? 0.03281= 560.25282m3(标) H2 V5H2 =17075.67272 ? 0.6225=10629.60627m3(标) N2 V5N2 =17075.67272 ? 0.2075=3543.20209m3(标)
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 =17075.67272 m3(标)
出塔物料：V8 =15183.47307 m3(标) 其中
NH3 V8NH3 =15183.47307 ?0.16=2429.3557m3(标) CH4 V8CH4 =15183.47307 ?0.13326=2023.34962m3(标) Ar V8AR =15183.47307 ?0.16=566.49538m3(标) H2 V8H2 =15183.47307 ?0.16=7623.16632m3(标) N2 V8N2 =15183.47307 ?0.16=2541.10605m3(标) 合成塔生成氨量： △ VNH3 = V8NH3-V5NH3
=2429.3557-341.51345 =2087.84225m3(标) =1586.6013kg
废热锅炉进出口物料，热交换器热气进出物料等于合成塔出塔物料，即V8 = V9= V10 =15183.47307 m3(标)
3.3.9 水冷器物料计算
进器物料：水冷器进气物料等于热交换器热气进出物料，即 V10入=15183.47307m3(标)
出器物料：在水冷器中部分气氨被冷凝，由氨分离器气液平衡计算得，气液比L/V= 8.72384 ,
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河南城建学院毕业论文（设计）
故有如下方程：
将V11出=8.72384L 11出 ，代入得： L 11出=
15183.47307?1561.46883m3(标)
9.72384V 11出=15183.47307-1561.46883=13621.53117m3(标) 出器气体组分由V11i=V11出y11i 其中
NH3 V11 NH3 =13621.53117?0.0681=927.62627m3(标) CH4 V11CH4 =13621.53117?0.14731=2006.58776m3(标) Ar V11AR =13621.53117?0.04143=564.34004m3(标) H2 V11H2 =13621.53117?0.55816=7602.99384m3(标) N2 V11N2 =13621.53117?0.185=2519.98327m3(标) 出器液体各组分由L 11i = V8i – V11i 其中
NH3 L11 NH3 =2429.3557-927.62627=1501.72943m3(标) CH4 L11CH4 =2023.34962-2006.58776=16.76186m3(标) Ar L11AR =566.49538-564.34004=2.15534m3(标) H2 L11H2 =7623.16623-7602.99384=20.17248m3(标) N2 L11N2 =2541.10605-2519.98327=21.12278m3(标)
3.3.10 氨分离器物料计算
进器物料：氨分离进器总物料等于水冷器出器气液混合物总物料。即V11 = V11出+L 11出=13621.53117+1561.46883=15183m3(标)
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=13621.53117m3(标) ， 出器液体：
L 15=L 11出=1561.46883m3(标) ，
氨分离器出口气体放空V13=172.39435m3(标)
其中 NH3 V13 NH3 =172.39435?0.0681=11.74006m3(标)
CH4V13CH4 =172.39435?0.14731=25.39541m3(标)
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河南城建学院毕业论文（设计）
ArV13AR =172.39435?0.04143=7.142298m3(标) H2V13H2 =172.39435?0.55816=96.22363m3(标) N2V13N2 =172.39435?0.185=31.89295m3(标)
3.3.11 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=13621.53117-172.39435=13449.13682m3(标)
其中 NH3V14 NH3 =13449.13682?0.0681=915.88622m3(标)
CH4V14CH4 =13449.13682?0.0681=1981.19232m3(标) ArV14AR =13449.13682?0.0681=557.19774m3(标) H2V14H2 =13449.13682?0.0681=7506.77021m3(标) N2V14N2 =13449.13682?0.0681=2488.09031m3(标) 出口物料（热气）：
设热气出口温度17℃，查t=17℃，p=28.42Mpa，气相中平衡氨含量y*=5.9%，计算热气出口冷凝液氨量时，忽略溶解在液氨中的气体。取过饱和度10﹪，故V17NH3=5.9﹪?1.1﹪=6.49﹪. 设热气出口氨体积为a，则：
a?0.0649
13449.13682?915.88622?aa=869.85251
冷交换器热气冷凝液氨量为：
L 17NH3=V14NH3 –a=915.88622-869.85251=46.03371m3(标) 冷交换器热气出口气量及组分
其中 NH3V17 NH3 =V14NH3 –L 17NH3 =915.88622-46.03371=869.85251 m3(标)
CH4V17CH4 =V14CH4=1981.19235 m3(标) ArV17AR =V14AR=557.19774 m3(标) H2V17H2 =V14H2=7506.77021 m3(标) N2V17N2 =V14N2=2488.09031
出口总气量V17=V14 –L 17NH3=13449.13682-46.03371=13403.10311 m3(标) 出口气体各组分：
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河南城建学院毕业论文（设计）
其中 NH3 V17NH3 /V17 =
869.85251?6.49%
13403.103111981.19235?14.782% CH4 V17CH4 /V1 7=
13403.10311557.19774?4.157% Ar V17AR /V1 7=
13403.103117506.77021?56.007% H2 V17H2 /V1 7=
13403.103112488.09031?18.564% N2 V17N2 /V17 =
13403.103113.3.12氨冷器物料计算
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=4199.84482m3(标)
其中 CH4 V1CH4 =4199.84482?0.01=41.99845m3(标)
Ar V1AR =4199.84482?0.0028=11.75957m3(标) H2 V1H2 =4199.84482?0.7404=3109.5651m3(标) N2 V1N2 =4199.84482?0.2648=1036.5217m3(标)
V18 =V1+V17=4199.84482+13403.10311=17602.94793m3(标) 进器气体组分含量V18i =V1i+V17i
其中 NH3 V18 NH3 =V17NH3=869.85251m3(标)
CH4 V18CH4 =41.99845+1981.19235=2023.1908m3(标) Ar V18AR =11.75957+557.19774=568.95731m3(标) H2 V18H2 =3109.5651+7506.77021=10616.33531m3(标) N2 V18N2 =1036.5217+2488.09031=3524.61201m3(标) 各组分百分含量y18i=V18i /V18
869.85251?0.04942
17602.947932023.1908?0.11493 CH4 y18CH4 =
17602.94793568.95731?0.03232 Ar y18AR =
17602.9479310616.33531?0.6031 H2 y18H2 =
17602.947933524.61201?0.20023 N2y18N2 =
17602.94793其中 NH3 y18NH3 =
进器液体等于冷交换器冷凝液氨量：
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河南城建学院毕业论文（设计）
L18 =L18NH3 =L 17NH3 =46.03371m3(标)
进器总物料=V18+L18 =17602.94793+46.03371=17648.98164m3(标) 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b，
b?0.02
17602.94793?869.85251解b =334.66191m3(标)
则氨冷器中冷凝液氨量：L 18= V18–b =869.85251-334.66191=535.1906 氨冷器出器总液氨量：L =46.03371+535.1906=581.22431m3(标)
氨冷器出器气体量：V2=V18–b=17602.94793-334.66191=17268.28602m3(标) 其中 NH3 V2NH3 =334.66191m3(标)
CH4 V2CH4 =V18CH4=2023.1908m3(标) Ar V2AR =V18AR=568.95731m3(标) H2 V2H2 =V18H2=10616.33531m3(标) N2 V2N2 =V18N2=3524.61201m3(标)
各组分百分含量y2i=V2i /V2
334.66191?1.938%
17268.286022023.1908?11.716% CH4 y2CH4 =
17268.28602568.95731?3.295% Ar y2AR =
17268.2860210616.33531?61.479% H2 y2H2 =
17268.286023524.61201?20.411% N2 y2N2 =
17268.286022NH3
= L 18NH3+ L 18NH3
其中 NH3 y2 NH3 =
出器总物料= V2 + L 2NH3 =17268.28602+581.22431=17849.51033m3(标) 交换器物料计算
进器物料：冷交换器进器总物料等于氨冷器出器总物料。其中气体入口V2 =17268.28602m3(标)，液体入口L 2NH3 =581.22431m3(标)，由气液平衡计算得：以1kmol进口物料为计算基准： 即F =1
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