四川理工学院毕业设计1(6)

四川理工学院毕业设计 工艺计算

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激液体量.

V3= V2′- L16

=13811.948 – 978.207= 12833.741 m3(标)

其中 NH3 V3NH3= 12833.741 3 0.03 =385.012 m3(标)

CH4 V3CH4= 12833.741 3 0.1004=1288.508 m(标)Ar V3Ar= 12833.741 3 0.0396 =508.216 m3(标) H2 V3H2= 12833.741 3 0.6225=7989.004 m3(标) N2 V3N2= 12833.741 3 0.2175=2791.339 m3(标)

计算误差=（V3-V5）/V5 3100％

=(12833.741-13231.663)/12833.7413100%=-3.101%

校核氨分离器分离液氨百分数 氨分离器分离液氨百分数

G分％=L15X15/(L15+L16X16)3100％

=750.35630.9591/(750.35630.9591 + 978.20730.98448)3100 =42.769％

冷交换器分离液氨百分数：G冷％=1-G分％=1-42.769%=57.231％ 计算误差=（G′-G分）/G′=(0.51897-0.42769)/0.42769=-2.134％

3

2.2.13液氨贮槽物料计算

进槽物料：氨分离器入槽液体 L15=750.356 m(标) 其中 NH3 L15NH3= 750.35630.9591 =719.666 m3(标)

CH4 L15CH4= 750.35630.01421 =10.663 m3(标) Ar L15Ar= 750.35630.00147 =1.103 m3(标) H2 L15H2= 750.35630.0196 =14.707 m3(标) N2 L15N2= 750.35630.00614 =4.607 m3(标)

冷交换器入槽液体L16=978.207 m3(标)

其中 NH3 L16NH3= 978.207 3 0.98448 =963.025 m3(标)

CH4 L16CH4= 978.207 3 0.00372 =3.639 m3(标) Ar L16Ar= 978.207 3 0.00078 =0.763 m(标)H2 L16H2= 978.207 3 0.0083 =8.119 m3(标) N2 L16N2= 978.2079 3 0.00272 =2.661 m3(标)

入槽混合物料 3

3

L21=L15+L16=750.356 + 978.207 =1728.563 m3(标)

各组分物料含量：L21i=L15i+L16i

其中 NH3 L21NH3= 719.734 + 963.025 =1682.759 m3(标)

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四川理工学院毕业设计 工艺计算

CH4 L21CH4= 10.854 + 3.639 =14.493 m3(标) Ar L21Ar= 1.094 + 0.763 =1.857 m3(标) H2 L21H2= 14.874 + 8.119 =22.993 m3(标) N2 L21N2= 3.809 + 2.661 =6.47 m3(标)

百分含量 Y21i=L21i/L21

其中 NH3 Y21NH3= 1682.759/1728.563=97.350％

CH4 Y21CH4= 14.493/1728.563=0.838% Ar Y21Ar= 1.857/1728.563=0.107% H2 Y21H2= 22.993/1728.563=1.330% N2 Y21N2= 6.47/1728.5637=0.374%

出槽物料：液氨贮槽出口弛放气 V20=92.352 m3(标) 其中 NH3 V20NH3= 92.352 30.58645 =54.160 m3(标)

CH4 V20CH4= 92.352 3 0.12678 =11.708 m3(标) Ar V20Ar= 92.352 3 0.01668 =1.540 m3(标) H2 V20H2= 92.352 3 0.20769 =19.181 m3(标) N2 V20N2= 92.352 3 0.06598 =6.093 m3(标)

出口液氨总物料 L19=L21-L20=1728.563 – 92.352 =1636.211 m3(标)

其中 NH3 L19NH3=L21NH3-V20NH3=1682.759 – 54.16 =1628.599 m3(标

CH4 L19CH4=L21CH4-V20CH4=14.493 – 11.708 =2.785 m3(标 Ar L19NH3=L21NH3-V20NH3=1.857 – 1.54 =0.317 m3(标 H2 L19H2=L21H2-V20H2=22.993 – 19.1811=3.812 m3(标 N2 L19N2=L21N2-V20N2=6.47 – 6.093 =0.377 m3(标

各组分百分含量：

Y19i=L19i/L19

其中 NH3 Y19NH3=1628.599/1636.211=99.535％

CH4 Y19CH4=2.785/1636.211=0.17021％ Ar Y19Ar=0.317/1636.211=0.0194％ H2 Y19H2=3.812/1636.211=0.233％ N2 Y19N2=0.377/1636.211=0.023％

液氨产量核算: NNH3=1628.599/22.4317=1235.99Kg

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四川理工学院毕业设计 工艺计算

2.2.14 物料衡算结果汇总

表 2-15

%

3

氨冷器出口气体2

m(标)/tNH3 m(标)/h Kmol/h 385.268

3

冷交换器冷气出口3/4/5

%

m(标)/tNH3 m(标)/h Kmol/h 385.012 1604.73 71.640 1288.508 5370.501 239.755 508.216 2118.244 94.564 7989.004 33298.169 1486.525 2791.339 11634.301 519.388

3

3

NH3 3.00 CH4 10.04 Ar 3.96 H2 62.25 N2 21.75

1605.797 71.687 3.00

1327.093 5531.324 246.934 10.04 526.539 8253.41

2194.615 97.974 3.96 34400.213 1535.724 62.25

2735.224 11400.414 508.947 21.75

合计 100.00 13227.534 55132.362 2461.266 100.00 12833.741 53491.032 2387.993

表 2-16

合成塔第二次出口8/9

% 15

m(标)/tNH3 m(标)/h Kmol/h 1777.557

7408.858 330.753 5536.884 247.182 2183.636 97.484 25697.375 1147.204 8565.628 382.394

3

3

%

合成塔第一次入口5/6/7

m(标)/tNH3 m(标)/h 396.95 1328.459 523.974 8236.71 2877.887

3

3

Kmol/h

NH3 3.00 CH4 10.04 Ar 3.96 H2 62.25 N2 21.75

1654.488 73.861

5537.017 247.188 11.21 1328.427 2183.924 97.497 4.421 523.905 34330.607 1532.616 52.027 6165.397 11995.033 535.493 17.342 2055.093

合计 100.00 13231.663 55149.571 2462.034 100.00 11850.379 49392.380 2205.017

表 2-17

%

水冷器出口气体10

m(标)/tNH3 m(标)/h Kmol/h 1057.823 1317.573 522.811 6150.523 2051.284

3

3

水冷器出口液体10

%

m(标)/tNH3 m(标)/h Kmol/h 719.734 10.854 1.094 14.874 3.809

2999.851 133.922 45.239 4.560 61.995 15.876

2.020 0.204 2.768 0709

3

3

NH3 9.53 CH4 11.87 Ar 4.71 H2 55.41 N2 18.48

4409.006 196.831 95.91 5491.644 245.163 1.421 2179.076 97.280

0.147

25635.380 1144.437 1.96 8549.752 381.685 0.614

合计 100.00 11100.023 46264.896 2065.397 100.00 750.356

表 2-18

3127.484 139.620

%

3

氨分离器出口11

m(标)/tNH3 m(标)/h Kmol/h 1057.823

3

放空气12

%

m(标)/tNH3 m(标)/h Kmol/h 8.794 10.953 4.346

36.653 45.652 18.114

1.636 2.038 0.809

3

3

NH3 9.53 Ar 4.71

4409.006 196.831 9.53 5491.644 245.163 11.87 2179.076 97.280 4.71

CH4 11.87 1317.573

522.811

四川理工学院毕业设计 工艺计算

H2 55.41 6150.523 N2 18.48 2051.284 合计 100.00 11100.023

%

25635.380 1144.437 55.41 8549.752 381.685 18.48 46264.896 2065.397 100.00

表 2-19

51.128 17.052 92.273

213.102 71.073 384.594

9.513 3.173 17.169

冷交换器热气进口13

m(标)/tNH3 m(标)/h Kmol/h

3

3

氨分离器出口液氨14

%

m(标)/tNH3 m(标)/h Kmol/h 719.734 10.854 1.094 14.874 3.809

2999.851 133.922 45.239 4.560 61.995 15.876

2.020 0.204 2.768 0709

3

3

NH3 9.53 CH4 11.87 Ar 4.71 H2 55.41 N2 18.48

1049.039 4372.395 195.196 95.91 1306.62 518.465

5445.992 243.125 1.421 2160.962 96.472

0.147

6099.394 25422.274 1134.923 1.96 2034.232 8478.679 378.512 0.614

Σ 100.00 11007.75 45880.302 2048.228 100.00 750.356 3127.484 139.620

表 2-20

%

冷交换器出口液氨15

m(标)/tNH3 m(标)/h Kmol/h 963.025 3.639 0.763 8.119 2.661 978.207

3

3

冷交换器热气出口16

%

m(标)/tNH3 m(标)/h Kmol/h 691.178 1306.62 518.465

2880.830 128.608 5445.992 243.125 2160.962 96.472

3

3

NH3 98.448 CH4 0.372 Ar 0.078 H2 0.83 N2 0.272 合计 100.00

%

4013.888 179.191 6.49 15.167 3.180 33.840 11.091

0.677 12.269 0.142

4.868

1.511 57.272 6099.394 25422.274 1134.923 0.495 19.101 2034.232 8478.679 378.512

4077.167 182.016 100.00 10649.889 44388.737 1981.640

表 2-21

冷交换器热气进口16

m(标)/tNH3 m(标)/h Kmol/h 357.861

357.861

3

3

氨冷器进口17

%

m(标)/tNH3 m(标)/h Kmol/h 691.178 2880.830 128.608 1327.093 5531.324 246.934 526.539 2194.615 97.974 8253.41 34400.213 1535.724 2735.224 11400.414 508.947 13533.444 56407.395 2518.187

3

3

NH3 100.00 CH4 Ar H2 N2 合计 100.00

%

3

1491.565 66.588 5.107

9.806 3.891 60.985 20.211

1491.565 66.588 100.00

表 2-22

氨冷器进口17

m(标)/tNH3 m(标)/h Kmol/h 357.861

3

液氨储槽出口18

%

m(标)/tNH3 m(标)/h Kmol/h 1317.647 5490.635 245.118

3

3

NH3 100.00 1491.565 66.588 99.874

四川理工学院毕业设计 工艺计算

CH4 Ar H2 N2 合计 100.00

%

357.861

0.076 0.003 0.036 0.011

1.003 0.04 0.475 0.145

4.181 0.167 1.980 0.604

0.187 0.007 0.088 0.27

1491.565 66.588 100.00

表 2-23

1319.309 5498.880 245.486

驰 放 气19

m(标)/tNH3 m(标)/h Kmol/h 54.160 11.708 1.54 19.181 6.093 92.352

3

3

液氨储槽进口20

%

m(标)/tNH3 m(标)/h Kmol/h 1371.807 5717.692 255.254 12.711 1.58 19.656 6.238

52.979 6.585 81.926 26.000

2.365 0.294 3.657 1.161

3

3

NH3 58.645 CH4 12.678 Ar 1.668 H2 20.769 N2 6.598 合计 100.00

%

3

225.739 10.078 97.131 48.799 6.419 79.946 25.396

2.179 0.00916 0.287 0.00114 3.569 0.01416 1.134 0.00449

384.923 17.417 100.00

表 2-24

1411.992 5885.183 262.731

补充新鲜气1

m(标)/tNH3 m(标)/h Kmol/h

20.473 8.074

85.331 33.652

3.809 1.502

3

氨冷器出口2

% 100.00

m(标)/tNH3 m(标)/h Kmol/h 663.771

663.771

2766.598 123.509

3

3

NH3 CH4 0.71 Ar 0.28 H2 74.70 N2 24.31

2154.016 8977.939 400.801 700.992

2921.735 130.435

合计 100.00 2883.556 12018.661 536.547 100.00 2766.598 123.509

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