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收稿日期:
2024-04-30
修回日期:
2024-07-06
出版日期:
2024-07-08
通讯作者:
王治红
作者简介:
向腾龙(1998—),男,硕士研究生,1569265168@qq.com
Tenglong XIANG1(), Zhihong WANG1(
), Gui WANG2, Long LI2
Received:
2024-04-30
Revised:
2024-07-06
Online:
2024-07-08
Contact:
Zhihong WANG
摘要:
为了从天然气发电厂的烟气中捕获二氧化碳(CO2)并回收液化天然气(LNG)的冷能,提出了一种分级回收 LNG 冷能的工艺。该工艺将液化天然气按温度分为深冷、中冷和浅冷,并将每一段冷能分别与循环介质相匹配,以回收LNG冷能、水和捕获CO2,同时向外界输送电力。在有机朗肯循环(ORC)中,热源是烟道气,冷源是液化天然气。系统的热力学分析表明,该系统的热回收效率、冷能利用率、发电效率和㶲效率分别为 41.55%、14.34%、10.80% 和 53.60%。CO2捕获量和冷能发电量分别为 177.30 kg/t LNG 和 25.86 kWh /t LNG。此外,还对LNG再气化压力进行了研究,在气化压力为 1.00 MPa时,CO2捕集率达到最大。较高的㶲效率表明了分级冷能利用工艺设计的新颖性以及工作流体在 ORC 中使用的适宜性。
中图分类号:
向腾龙, 王治红, 汪贵, 李龙. 液化天然气冷能梯级利用的多功能集成系统研究[J]. 化工学报, DOI: 10.11949/0438-1157.20240479.
Tenglong XIANG, Zhihong WANG, Gui WANG, Long LI. Research on multifunctional integrated system for cold energy cascade utilization of liquefied natural gas[J]. CIESC Journal, DOI: 10.11949/0438-1157.20240479.
参数 | 数值 |
---|---|
LNG温度/℃ | -162.00 |
LNG压力/kPa | 200.00 |
工艺水进口温度/℃ | 25.00 |
冷冻水出口温度/℃ | 7.00 |
工艺水压力/kPa | 100.00 |
LNG质量流量/(kg/s) | 5.00 |
表1 系统所需的热力学参数
Table 1 Thermodynamic parameters required for the system
参数 | 数值 |
---|---|
LNG温度/℃ | -162.00 |
LNG压力/kPa | 200.00 |
工艺水进口温度/℃ | 25.00 |
冷冻水出口温度/℃ | 7.00 |
工艺水压力/kPa | 100.00 |
LNG质量流量/(kg/s) | 5.00 |
组分 | 甲烷 | 乙烷 | 丙烷 | 氮气 |
---|---|---|---|---|
摩尔分率/% | 90.38 | 5.37 | 4.04 | 0.21 |
表2 LNG组分摩尔分率[27]
Table 2 Molar fraction of LNG components
组分 | 甲烷 | 乙烷 | 丙烷 | 氮气 |
---|---|---|---|---|
摩尔分率/% | 90.38 | 5.37 | 4.04 | 0.21 |
参数 | 数值 |
---|---|
温度/℃ | 87.50 |
压力/kPa | 300.00 |
组分 | 摩尔分率/% |
N2 | 76.30 |
CO2 | 6.00 |
O2 | 5.90 |
H2O | 11.80 |
表3 废气余热的进口条件和组成[28]
Table 3 Inlet conditions and composition of exhaust gas waste heat
参数 | 数值 |
---|---|
温度/℃ | 87.50 |
压力/kPa | 300.00 |
组分 | 摩尔分率/% |
N2 | 76.30 |
CO2 | 6.00 |
O2 | 5.90 |
H2O | 11.80 |
工质 | 化学式 | 正常沸点/℃ |
---|---|---|
甲烷 | CH4 | -161.50 |
R1150 | C2H4 | -103.70 |
R170 | C2H6 | -88.60 |
R1270 | C3H6 | -47.70 |
R290 | C3H8 | -42.170 |
R600a | i-C4H10 | -12.40 |
R600 | n-C4H10 | -0.50 |
表4 工质的热力学性质[29]
Table 4 Thermodynamic properties of the substances
工质 | 化学式 | 正常沸点/℃ |
---|---|---|
甲烷 | CH4 | -161.50 |
R1150 | C2H4 | -103.70 |
R170 | C2H6 | -88.60 |
R1270 | C3H6 | -47.70 |
R290 | C3H8 | -42.170 |
R600a | i-C4H10 | -12.40 |
R600 | n-C4H10 | -0.50 |
编号 | 气相分率 | 温度/℃ | 压力/ kPa | 摩尔流量/(kmol/h) | 质量流量/(kg/h) | 质量焓/(kJ/kg) | 质量熵/[kJ/(kg·K)] | 质量有效能/(kJ/kg) |
---|---|---|---|---|---|---|---|---|
LNG | 0.00 | -162.00 | 200.00 | 1002.52 | 18000.00 | -5143.90 | 4.19 | 961.43 |
L1 | 0.00 | -161.63 | 1000.00 | 1002.52 | 18000.00 | -5141.73 | 4.19 | 961.93 |
L2 | 0.47 | -120.00 | 1000.00 | 1002.52 | 18000.00 | -4831.14 | 6.38 | 621.57 |
L3 | 0.94 | -84.65 | 1000.00 | 1002.52 | 18000.00 | -4555.77 | 8.06 | 395.06 |
L4 | 1.00 | -61.32 | 1000.00 | 1002.52 | 18000.00 | -4454.77 | 8.56 | 345.81 |
NG | 1.00 | 20.00 | 1000.00 | 1002.52 | 18000.00 | -4280.79 | 9.26 | 312.76 |
1 | 1.00 | -90.69 | 3600.00 | 723.06 | 11600.00 | -5049.65 | 8.01 | 643.00 |
2 | 0.83 | -110.35 | 1800.00 | 723.06 | 11600.00 | -5077.63 | 8.05 | 602.21 |
3 | 0.00 | -156.58 | 1800.00 | 723.06 | 11600.00 | -5559.58 | 4.90 | 1058.77 |
4 | 0.00 | -155.64 | 3600.00 | 723.06 | 11600.00 | -5554.20 | 4.91 | 1060.13 |
5 | 0.00 | -75.07 | 200.00 | 335.63 | 10092.12 | -3448.63 | 4.02 | 326.67 |
6 | 0.00 | -74.55 | 1000.00 | 335.63 | 10092.12 | -3446.72 | 4.02 | 327.81 |
7 | 1.00 | 0.00 | 1000.00 | 335.63 | 10092.12 | -2880.52 | 6.40 | 184.45 |
8 | 1.00 | -60.83 | 200.00 | 335.63 | 10092.12 | -2957.47 | 6.49 | 79.63 |
9 | 0.00 | -42.75 | 100.00 | 90.71 | 4000.00 | -2916.64 | 4.09 | 137.17 |
10 | 0.00 | -42.33 | 800.00 | 90.71 | 4000.00 | -2915.13 | 4.09 | 138.18 |
11 | 1.00 | 40.00 | 800.00 | 90.71 | 4000.00 | -2381.88 | 5.98 | 110.02 |
12 | 1.00 | -20.83 | 100.00 | 90.71 | 4000.00 | -2462.14 | 6.06 | 5.38 |
13 | 0.00 | -32.14 | 1000.00 | 249.42 | 7500.00 | -3333.46 | 4.53 | 287.45 |
14 | 0.00 | -31.12 | 2000.00 | 249.42 | 7500.00 | -3330.76 | 4.54 | 289.33 |
15 | 1.00 | 15.00 | 2000.00 | 249.42 | 7500.00 | -2879.30 | 6.24 | 232.53 |
16 | 1.00 | -18.10 | 1000.00 | 249.42 | 7500.00 | -2913.17 | 6.28 | 188.67 |
Flue Gas | 1.00 | 87.50 | 300.00 | 1391.45 | 39000.00 | -1794.50 | 5.55 | 108.56 |
F1 | 0.98 | 68.16 | 300.00 | 1391.45 | 39000.00 | -1849.19 | 5.40 | 100.93 |
F2 | 1.00 | 68.16 | 300.00 | 1360.65 | 38445.07 | -1649.26 | 5.42 | 102.21 |
F3 | 0.92 | 39.01 | 300.00 | 1360.65 | 38445.07 | -1797.89 | 4.97 | 88.31 |
F4 | 1.00 | 39.01 | 300.00 | 1257.29 | 36582.82 | -1083.83 | 5.06 | 92.64 |
F5 | 0.98 | -9.21 | 300.00 | 1257.29 | 36582.82 | -1169.43 | 4.77 | 94.67 |
F6 | 1.00 | -9.21 | 300.00 | 1228.51 | 36064.20 | -955.74 | 4.80 | 93.70 |
F7 | 0.94 | -131.07 | 300.00 | 1228.51 | 36064.20 | -1118.02 | 3.93 | 191.85 |
F8 | 0.00 | -131.07 | 300.00 | 74.26 | 3228.13 | -9520.99 | 0.98 | 319.51 |
F9 | 1.00 | -131.07 | 300.00 | 1154.25 | 32836.07 | -291.92 | 4.22 | 160.90 |
F10 | 1.00 | -37.15 | 300.00 | 1154.25 | 32836.07 | -195.93 | 4.74 | 102.24 |
Tail Gas | 1.00 | 20.00 | 300.00 | 1154.25 | 32836.07 | -137.17 | 4.96 | 94.54 |
H1 | 0.00 | 68.16 | 300.00 | 30.80 | 554.93 | -15699.92 | 3.57 | 12.57 |
H2 | 0.00 | 39.01 | 300.00 | 103.36 | 1862.24 | -15825.32 | 3.18 | 1.62 |
H3 | 0.00 | -9.21 | 300.00 | 28.78 | 518.63 | -16029.15 | 2.46 | 9.41 |
CW-IN-1 | 0.00 | 25.00 | 100.00 | 2419.32 | 43584.35 | -15887.82 | 2.98 | 0.00 |
CW-OUT-1 | 0.00 | 7.00 | 100.00 | 2419.32 | 43584.35 | -15965.51 | 2.71 | 2.44 |
CW-IN-2 | 0.00 | 25.00 | 100.00 | 1378.59 | 24835.47 | -15887.82 | 2.98 | 0.00 |
CW-OUT-2 | 0.00 | 7.00 | 100.00 | 1378.59 | 24835.47 | -15965.51 | 2.71 | 2.44 |
表5 模拟过程的热力学数据
Table 5 Thermodynamic data of the simulated process
编号 | 气相分率 | 温度/℃ | 压力/ kPa | 摩尔流量/(kmol/h) | 质量流量/(kg/h) | 质量焓/(kJ/kg) | 质量熵/[kJ/(kg·K)] | 质量有效能/(kJ/kg) |
---|---|---|---|---|---|---|---|---|
LNG | 0.00 | -162.00 | 200.00 | 1002.52 | 18000.00 | -5143.90 | 4.19 | 961.43 |
L1 | 0.00 | -161.63 | 1000.00 | 1002.52 | 18000.00 | -5141.73 | 4.19 | 961.93 |
L2 | 0.47 | -120.00 | 1000.00 | 1002.52 | 18000.00 | -4831.14 | 6.38 | 621.57 |
L3 | 0.94 | -84.65 | 1000.00 | 1002.52 | 18000.00 | -4555.77 | 8.06 | 395.06 |
L4 | 1.00 | -61.32 | 1000.00 | 1002.52 | 18000.00 | -4454.77 | 8.56 | 345.81 |
NG | 1.00 | 20.00 | 1000.00 | 1002.52 | 18000.00 | -4280.79 | 9.26 | 312.76 |
1 | 1.00 | -90.69 | 3600.00 | 723.06 | 11600.00 | -5049.65 | 8.01 | 643.00 |
2 | 0.83 | -110.35 | 1800.00 | 723.06 | 11600.00 | -5077.63 | 8.05 | 602.21 |
3 | 0.00 | -156.58 | 1800.00 | 723.06 | 11600.00 | -5559.58 | 4.90 | 1058.77 |
4 | 0.00 | -155.64 | 3600.00 | 723.06 | 11600.00 | -5554.20 | 4.91 | 1060.13 |
5 | 0.00 | -75.07 | 200.00 | 335.63 | 10092.12 | -3448.63 | 4.02 | 326.67 |
6 | 0.00 | -74.55 | 1000.00 | 335.63 | 10092.12 | -3446.72 | 4.02 | 327.81 |
7 | 1.00 | 0.00 | 1000.00 | 335.63 | 10092.12 | -2880.52 | 6.40 | 184.45 |
8 | 1.00 | -60.83 | 200.00 | 335.63 | 10092.12 | -2957.47 | 6.49 | 79.63 |
9 | 0.00 | -42.75 | 100.00 | 90.71 | 4000.00 | -2916.64 | 4.09 | 137.17 |
10 | 0.00 | -42.33 | 800.00 | 90.71 | 4000.00 | -2915.13 | 4.09 | 138.18 |
11 | 1.00 | 40.00 | 800.00 | 90.71 | 4000.00 | -2381.88 | 5.98 | 110.02 |
12 | 1.00 | -20.83 | 100.00 | 90.71 | 4000.00 | -2462.14 | 6.06 | 5.38 |
13 | 0.00 | -32.14 | 1000.00 | 249.42 | 7500.00 | -3333.46 | 4.53 | 287.45 |
14 | 0.00 | -31.12 | 2000.00 | 249.42 | 7500.00 | -3330.76 | 4.54 | 289.33 |
15 | 1.00 | 15.00 | 2000.00 | 249.42 | 7500.00 | -2879.30 | 6.24 | 232.53 |
16 | 1.00 | -18.10 | 1000.00 | 249.42 | 7500.00 | -2913.17 | 6.28 | 188.67 |
Flue Gas | 1.00 | 87.50 | 300.00 | 1391.45 | 39000.00 | -1794.50 | 5.55 | 108.56 |
F1 | 0.98 | 68.16 | 300.00 | 1391.45 | 39000.00 | -1849.19 | 5.40 | 100.93 |
F2 | 1.00 | 68.16 | 300.00 | 1360.65 | 38445.07 | -1649.26 | 5.42 | 102.21 |
F3 | 0.92 | 39.01 | 300.00 | 1360.65 | 38445.07 | -1797.89 | 4.97 | 88.31 |
F4 | 1.00 | 39.01 | 300.00 | 1257.29 | 36582.82 | -1083.83 | 5.06 | 92.64 |
F5 | 0.98 | -9.21 | 300.00 | 1257.29 | 36582.82 | -1169.43 | 4.77 | 94.67 |
F6 | 1.00 | -9.21 | 300.00 | 1228.51 | 36064.20 | -955.74 | 4.80 | 93.70 |
F7 | 0.94 | -131.07 | 300.00 | 1228.51 | 36064.20 | -1118.02 | 3.93 | 191.85 |
F8 | 0.00 | -131.07 | 300.00 | 74.26 | 3228.13 | -9520.99 | 0.98 | 319.51 |
F9 | 1.00 | -131.07 | 300.00 | 1154.25 | 32836.07 | -291.92 | 4.22 | 160.90 |
F10 | 1.00 | -37.15 | 300.00 | 1154.25 | 32836.07 | -195.93 | 4.74 | 102.24 |
Tail Gas | 1.00 | 20.00 | 300.00 | 1154.25 | 32836.07 | -137.17 | 4.96 | 94.54 |
H1 | 0.00 | 68.16 | 300.00 | 30.80 | 554.93 | -15699.92 | 3.57 | 12.57 |
H2 | 0.00 | 39.01 | 300.00 | 103.36 | 1862.24 | -15825.32 | 3.18 | 1.62 |
H3 | 0.00 | -9.21 | 300.00 | 28.78 | 518.63 | -16029.15 | 2.46 | 9.41 |
CW-IN-1 | 0.00 | 25.00 | 100.00 | 2419.32 | 43584.35 | -15887.82 | 2.98 | 0.00 |
CW-OUT-1 | 0.00 | 7.00 | 100.00 | 2419.32 | 43584.35 | -15965.51 | 2.71 | 2.44 |
CW-IN-2 | 0.00 | 25.00 | 100.00 | 1378.59 | 24835.47 | -15887.82 | 2.98 | 0.00 |
CW-OUT-2 | 0.00 | 7.00 | 100.00 | 1378.59 | 24835.47 | -15965.51 | 2.71 | 2.44 |
设备 | 位号 | 计算公式 | 㶲损失/kW | 㶲效率/% |
---|---|---|---|---|
泵 | P-100 | IP-100=ELNG +WP-100 -EL1 | 8.34 | 99.83 |
P-101 | IP-101 =E3 +WP-101 -E4 | 12.97 | 99.62 | |
P-102 | IP-102 =E5 +WP-102 -E6 | 2.15 | 99.77 | |
P-103 | IP-103=E9 +WP-103 -E10 | 0.54 | 99.65 | |
P-104 | IP-104=E13 +WP-104 -E14 | 1.73 | 99.71 | |
涡轮机 | K-100 | IK-100 =E1-WK-100 -E2 | 41.28 | 98.01 |
K-101 | IK-101 =E7-WK-101 -E8 | 78.15 | 84.89 | |
K-102 | IK-102 =E11-WK-102 -E12 | 27.09 | 77.84 | |
K-103 | IK-103 =E15-WK-103 -E16 | 20.81 | 95.70 | |
换热器 | HE-100 | IHE-100 = EL1 +E2-EL2 -E3 | 230.67 | 96.58 |
HE-101 | IHE-101 = EF6 +E4-EF7 -E1 | 360.82 | 91.71 | |
HE-102 | IHE-102 = EL2 +E8-EL3 -E5 | 440.05 | 86.79 | |
HE-103 | IHE-103 = EF2 +E6-EF3 -E7 | 550.36 | 72.63 | |
HE-104 | IHE-104 = EL3 +E12-EL4 -E9 | 99.81 | 94.96 | |
HE-105 | IHE-105 = E10 +EFlue gas-EF1 -E11 | 113.88 | 91.44 | |
HE-106 | IHE-106 = EF4 +EL4-EF5 -ENG | 144.58 | 94.59 | |
HE-107 | IHE-107 = EF9 +E16-EF10 -E13 | 329.20 | 82.31 | |
HE-108 | IHE-108 = E14 +ECW-IN-1-E15 -ECW-OUT-1 | 88.74 | 85.28 | |
HE-109 | IHE-109 = EF10 +ECW-IN-2-ETail gas -ECW-OUT-2 | 53.39 | 94.28 | |
分离器 | V-100 | IV-100 =EF1-EF2 -EH1 | 0.00 | 1.00 |
V-101 | IV-101 =EF3-EF4 -EH2 | 0.81 | 99.91 | |
V-102 | IV-102 =EF5-EF6 -EH3 | 22.05 | 97.71 | |
V-103 | IV-103 =EF7-EF8 -EF9 | 167.88 | 91.27 |
表6 各设备的㶲损失及㶲效率
Table 5 Losses and efficiencies for each piece of equipment
设备 | 位号 | 计算公式 | 㶲损失/kW | 㶲效率/% |
---|---|---|---|---|
泵 | P-100 | IP-100=ELNG +WP-100 -EL1 | 8.34 | 99.83 |
P-101 | IP-101 =E3 +WP-101 -E4 | 12.97 | 99.62 | |
P-102 | IP-102 =E5 +WP-102 -E6 | 2.15 | 99.77 | |
P-103 | IP-103=E9 +WP-103 -E10 | 0.54 | 99.65 | |
P-104 | IP-104=E13 +WP-104 -E14 | 1.73 | 99.71 | |
涡轮机 | K-100 | IK-100 =E1-WK-100 -E2 | 41.28 | 98.01 |
K-101 | IK-101 =E7-WK-101 -E8 | 78.15 | 84.89 | |
K-102 | IK-102 =E11-WK-102 -E12 | 27.09 | 77.84 | |
K-103 | IK-103 =E15-WK-103 -E16 | 20.81 | 95.70 | |
换热器 | HE-100 | IHE-100 = EL1 +E2-EL2 -E3 | 230.67 | 96.58 |
HE-101 | IHE-101 = EF6 +E4-EF7 -E1 | 360.82 | 91.71 | |
HE-102 | IHE-102 = EL2 +E8-EL3 -E5 | 440.05 | 86.79 | |
HE-103 | IHE-103 = EF2 +E6-EF3 -E7 | 550.36 | 72.63 | |
HE-104 | IHE-104 = EL3 +E12-EL4 -E9 | 99.81 | 94.96 | |
HE-105 | IHE-105 = E10 +EFlue gas-EF1 -E11 | 113.88 | 91.44 | |
HE-106 | IHE-106 = EF4 +EL4-EF5 -ENG | 144.58 | 94.59 | |
HE-107 | IHE-107 = EF9 +E16-EF10 -E13 | 329.20 | 82.31 | |
HE-108 | IHE-108 = E14 +ECW-IN-1-E15 -ECW-OUT-1 | 88.74 | 85.28 | |
HE-109 | IHE-109 = EF10 +ECW-IN-2-ETail gas -ECW-OUT-2 | 53.39 | 94.28 | |
分离器 | V-100 | IV-100 =EF1-EF2 -EH1 | 0.00 | 1.00 |
V-101 | IV-101 =EF3-EF4 -EH2 | 0.81 | 99.91 | |
V-102 | IV-102 =EF5-EF6 -EH3 | 22.05 | 97.71 | |
V-103 | IV-103 =EF7-EF8 -EF9 | 167.88 | 91.27 |
系统 | 消耗㶲 /kW | 有效㶲/kW | 㶲损失/kW | 㶲效率/% |
---|---|---|---|---|
ORC1 | 5765.69 | 5119.95 | 645.74 | 88.80 |
ORC2 | 4204.74 | 3134.03 | 1070.71 | 74.54 |
ORC3 | 3153.00 | 2911.68 | 241.32 | 92.35 |
ORC4 | 1473.18 | 1032.70 | 440.48 | 70.10 |
CO2 捕集 | 7786.64 | 6043.68 | 1742.96 | 77.62 |
LNG气化 | 7929.08 | 7005.63 | 923.45 | 88.35 |
整个系统 | 6024.05 | 3228.76 | 2795.29 | 53.60 |
表7 各系统㶲损失和㶲效率
Table 7 Losses and efficiencies of the systems
系统 | 消耗㶲 /kW | 有效㶲/kW | 㶲损失/kW | 㶲效率/% |
---|---|---|---|---|
ORC1 | 5765.69 | 5119.95 | 645.74 | 88.80 |
ORC2 | 4204.74 | 3134.03 | 1070.71 | 74.54 |
ORC3 | 3153.00 | 2911.68 | 241.32 | 92.35 |
ORC4 | 1473.18 | 1032.70 | 440.48 | 70.10 |
CO2 捕集 | 7786.64 | 6043.68 | 1742.96 | 77.62 |
LNG气化 | 7929.08 | 7005.63 | 923.45 | 88.35 |
整个系统 | 6024.05 | 3228.76 | 2795.29 | 53.60 |
F8 | F9 | |||
---|---|---|---|---|
组分 | 摩尔流量/ (kmol/h) | 摩尔分率/ % | 摩尔流量/ (kmol/h) | 摩尔分率/ % |
N2 | 0.4010 | 0.54 | 1061.2712 | 91.94 |
CO2 | 72.5341 | 97.67 | 10.9368 | 0.95 |
O2 | 0.0531 | 0.07 | 82.0424 | 7.11 |
H2O | 1.2762 | 1.72 | 0.0000 | 0.00 |
表8 流股F8和F9的摩尔组成
Table 8 Molar composition of flow stocks F8 and F9
F8 | F9 | |||
---|---|---|---|---|
组分 | 摩尔流量/ (kmol/h) | 摩尔分率/ % | 摩尔流量/ (kmol/h) | 摩尔分率/ % |
N2 | 0.4010 | 0.54 | 1061.2712 | 91.94 |
CO2 | 72.5341 | 97.67 | 10.9368 | 0.95 |
O2 | 0.0531 | 0.07 | 82.0424 | 7.11 |
H2O | 1.2762 | 1.72 | 0.0000 | 0.00 |
设备位号 | 消耗㶲/kW | 有效㶲/kW | 㶲损失/kW | 换热效率/% |
---|---|---|---|---|
HE-100 | 6750.12 | 6519.45 | 230.67 | 96.58 |
HE-101 | 4354.65 | 3993.83 | 360.82 | 91.71 |
HE-102 | 3331.10 | 2891.05 | 440.05 | 86.79 |
HE-103 | 2010.50 | 1460.14 | 550.36 | 72.63 |
HE-104 | 1981.26 | 1881.45 | 99.81 | 94.96 |
HE-105 | 1329.59 | 1215.71 | 113.88 | 91.44 |
HE-106 | 2670.43 | 2525.86 | 144.58 | 94.59 |
HE-107 | 1860.63 | 1531.43 | 329.20 | 82.31 |
HE-108 | 602.75 | 514.00 | 88.74 | 85.28 |
HE-109 | 932.56 | 879.17 | 53.39 | 94.28 |
表9 换热器的换热效率
Table 9 Heat transfer efficiency of heat exchangers
设备位号 | 消耗㶲/kW | 有效㶲/kW | 㶲损失/kW | 换热效率/% |
---|---|---|---|---|
HE-100 | 6750.12 | 6519.45 | 230.67 | 96.58 |
HE-101 | 4354.65 | 3993.83 | 360.82 | 91.71 |
HE-102 | 3331.10 | 2891.05 | 440.05 | 86.79 |
HE-103 | 2010.50 | 1460.14 | 550.36 | 72.63 |
HE-104 | 1981.26 | 1881.45 | 99.81 | 94.96 |
HE-105 | 1329.59 | 1215.71 | 113.88 | 91.44 |
HE-106 | 2670.43 | 2525.86 | 144.58 | 94.59 |
HE-107 | 1860.63 | 1531.43 | 329.20 | 82.31 |
HE-108 | 602.75 | 514.00 | 88.74 | 85.28 |
HE-109 | 932.56 | 879.17 | 53.39 | 94.28 |
图5 LNG再气化压力对系统性能的影响注:(a)能量变化;(b)热回收效率变化;(c)发电效率变化;(d)冷能利用率变化;(e)㶲损失变化
Fig. 5 Effect of LNG regasification pressure on system performance(a) Change in energy; (b) Change in heat recovery efficiency; (c) Change in power generation efficiency; (d) Change in cold energy utilization; (e) Change in exergy losses
作者 | 㶲效率/% | CO2捕获量/(kg/t LNG) | 发电量/(kWh/t LNG) |
---|---|---|---|
本论文 | 53.60 | 177.30 | 25.86 |
Xue[ | 25.70 | / | 24.00 |
Sun[ | 38.90 | / | 84.00 |
Zhang[ | 51.60 | 114.70 | 380.70 |
Xiong[ | 50.00 | 27.59 | 836.00 |
表10 系统结果比较
Table 10 Comparison of system results
作者 | 㶲效率/% | CO2捕获量/(kg/t LNG) | 发电量/(kWh/t LNG) |
---|---|---|---|
本论文 | 53.60 | 177.30 | 25.86 |
Xue[ | 25.70 | / | 24.00 |
Sun[ | 38.90 | / | 84.00 |
Zhang[ | 51.60 | 114.70 | 380.70 |
Xiong[ | 50.00 | 27.59 | 836.00 |
项目 | 单位 | 数值 |
---|---|---|
总资本成本 | USD | 4400120.00 |
总运营成本 | USD/year | 1068030.00 |
公用工程总成本 | USD/year | 33760.00 |
设备总成本 | USD | 1234000.00 |
期望回报率 | %/year | 20.00 |
表11 系统经济分析
Table 11 System economic analysis
项目 | 单位 | 数值 |
---|---|---|
总资本成本 | USD | 4400120.00 |
总运营成本 | USD/year | 1068030.00 |
公用工程总成本 | USD/year | 33760.00 |
设备总成本 | USD | 1234000.00 |
期望回报率 | %/year | 20.00 |
设备名称 | 设备位号 | 设备成本/USD | 设备重量/LBS | 公用工程成本/[USD/h] |
---|---|---|---|---|
涡轮机 | K-100 | 149000.00 | 9200.00 | 0.00 |
K-101 | 211000.00 | 10400.00 | 0.00 | |
K-102 | 148500.00 | 9300.00 | 0.00 | |
K-103 | 139300.00 | 9000.00 | 0.00 | |
泵 | P-100 | 26400.00 | 1600.00 | 1.16 |
P-101 | 73300.00 | 3200.00 | 1.73 | |
P-102 | 23200.00 | 1300.00 | 0.58 | |
P-103 | 21400.00 | 1000.00 | 0.17 | |
P-104 | 54200.00 | 2000.00 | 0.58 | |
分离器 | V-100 | 35800.00 | 4900.00 | 0.00 |
V-101 | 35800.00 | 4900.00 | 0.00 | |
V-102 | 34700.00 | 4600.00 | 0.00 | |
V-103 | 27000.00 | 3300.00 | 0.00 | |
换热器 | E-100 | 34200.00 | 5800.00 | 0.00 |
E-101 | 17400.00 | 3000.00 | 0.00 | |
E-102 | 57200.00 | 9700.00 | 0.00 | |
E-103 | 31700.00 | 5400.00 | 0.00 | |
E-104 | 21600.00 | 3700.00 | 0.00 | |
E-105 | 13200.00 | 2300.00 | 0.00 | |
E-106 | 13300.00 | 2300.00 | 0.00 | |
E-107 | 20100.00 | 3400.00 | 0.00 | |
E-108 | 30400.00 | 5200.00 | 0.00 | |
E-109 | 15300.00 | 2600.00 | 0.00 |
表12 各设备具体成本
Table 12 Equipment specific costs
设备名称 | 设备位号 | 设备成本/USD | 设备重量/LBS | 公用工程成本/[USD/h] |
---|---|---|---|---|
涡轮机 | K-100 | 149000.00 | 9200.00 | 0.00 |
K-101 | 211000.00 | 10400.00 | 0.00 | |
K-102 | 148500.00 | 9300.00 | 0.00 | |
K-103 | 139300.00 | 9000.00 | 0.00 | |
泵 | P-100 | 26400.00 | 1600.00 | 1.16 |
P-101 | 73300.00 | 3200.00 | 1.73 | |
P-102 | 23200.00 | 1300.00 | 0.58 | |
P-103 | 21400.00 | 1000.00 | 0.17 | |
P-104 | 54200.00 | 2000.00 | 0.58 | |
分离器 | V-100 | 35800.00 | 4900.00 | 0.00 |
V-101 | 35800.00 | 4900.00 | 0.00 | |
V-102 | 34700.00 | 4600.00 | 0.00 | |
V-103 | 27000.00 | 3300.00 | 0.00 | |
换热器 | E-100 | 34200.00 | 5800.00 | 0.00 |
E-101 | 17400.00 | 3000.00 | 0.00 | |
E-102 | 57200.00 | 9700.00 | 0.00 | |
E-103 | 31700.00 | 5400.00 | 0.00 | |
E-104 | 21600.00 | 3700.00 | 0.00 | |
E-105 | 13200.00 | 2300.00 | 0.00 | |
E-106 | 13300.00 | 2300.00 | 0.00 | |
E-107 | 20100.00 | 3400.00 | 0.00 | |
E-108 | 30400.00 | 5200.00 | 0.00 | |
E-109 | 15300.00 | 2600.00 | 0.00 |
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