Design and analysis of a new type of dual-pressure Linde-Hampson hydrogen liquefaction process

doi:10.16085/j.issn.1000-6613.2021-0060

Abstract

Abstract:

In order to reduce the production energy consumption and investment cost of hydrogen liquefaction plants and accelerate the development of hydrogen energy commercialization and civilian use in China, a novel dual-pressure Linde-Hampson (L-H) hydrogen liquefaction process using LNG pre-cooling is proposed. The designed liquid hydrogen output of the system is 5t/d and the method combining expansion and cooling with heat exchange is adopted to realize deep cooling of hydrogen. Aspen HYSYS software is used to carry out detailed simulation calculation and analysis for the process. The results show that the specific energy consumption and exergy efficiency of the hydrogen liquefaction process are 9.802 and 41.4%, respectively, and the total exergy loss of the process is 1373.3kW, of which the exergy loss of the heat exchange system accounts for the main part. It is found from the sensitivity analysis of the key parameters in the process that the change of the pre-compression pressure of the hydrogen in the range of 2—4MPa has a greater impact on the specific energy consumption and hydrogen liquefaction rate of the liquefaction process, while the pressure of LNG has little impact on the system. The novel hydrogen liquefaction process has simple equipment, low investment cost, and better liquefaction performance. It has advantages in the construction of small and medium-sized hydrogen liquefaction plants.

Key words: hydrogen liquefaction, HYSYS software, liquefied natural gas (LNG) pre-cooling, exergy analysis, sensitivity analysis

摘要：

为降低氢液化厂的生产能耗与投资成本，加快我国氢能商业化、民用化的发展，本文提出了一种采用液化天然气（LNG）预冷的新型双压Linde-Hampson（L-H）氢液化工艺系统。系统的设计液氢产量为5t/d，采用膨胀降温与换热冷却相结合的方法实现了对氢气的深冷。借助Aspen HYSYS软件对工艺流程展开了详细的模拟计算与分析，结果表明，该氢液化系统的比能耗为9.802，?效率为41.4%，系统的总?损失为1373.3kW，其中换热设备的?损失占主要部分；在对系统中关键参数进行的灵敏度分析中发现，氢气预压缩压力在2~4MPa范围内变化对液化系统的比能耗和氢气液化率影响较大，而LNG的加压压力对系统性能影响较小。新型氢液化工艺系统设备简单，投资成本较低，具备良好的液化性能，在未来中小型氢液化厂的建设中优势明显。

关键词: 氢液化, HYSYS软件, 液化天然气预冷, ?分析, 灵敏度分析

CLC Number:

TK91

CAO Xuewen, YANG Jian, BIAN Jiang, LIU Yang, GUO Dan, LI Qigui. Design and analysis of a new type of dual-pressure Linde-Hampson hydrogen liquefaction process[J]. Chemical Industry and Engineering Progress, 2021, 40(12): 6663-6669.

曹学文, 杨健, 边江, 刘杨, 郭丹, 李琦瑰. 新型双压Linde-Hampson氢液化工艺设计与分析[J]. 化工进展, 2021, 40(12): 6663-6669.

Figures/Tables 14

设备	?方程
压缩机	$Δ E C o m = E i n - E o u t = m ˙ C o m, i n × e C o m, i n + W C o m - m ˙ C o m, o u t × e C o m, o u t$
冷却器	$Δ E C = E i n - E o u t = m ˙ C, i n × (e C, i n - e C, i n)$
多流换热器	$Δ E H X = E i, i n - E i, o u t = ∑ i = 1 n m ˙ i × (e i, i n - e i, o u t)$
膨胀机	$Δ E E = E i n - E o u t = m ˙ E, i n × e E, i n - m ˙ E, o u t × e E, o u t - W E$
LNG泵	$Δ E P = E i n - E o u t = m ˙ P, i n × e P, i n + W P - m ˙ P, o u t × e P, o u t$
转化器	$Δ E C o = E i n - E o u t = m ˙ C o, i n × e C o, i n - ∑ i = 1 n m ˙ C o_i, o u t × e C o_i, o u t$

设备	?方程
压缩机	$Δ E C o m = E i n - E o u t = m ˙ C o m, i n × e C o m, i n + W C o m - m ˙ C o m, o u t × e C o m, o u t$
冷却器	$Δ E C = E i n - E o u t = m ˙ C, i n × (e C, i n - e C, i n)$
多流换热器	$Δ E H X = E i, i n - E i, o u t = ∑ i = 1 n m ˙ i × (e i, i n - e i, o u t)$
膨胀机	$Δ E E = E i n - E o u t = m ˙ E, i n × e E, i n - m ˙ E, o u t × e E, o u t - W E$
LNG泵	$Δ E P = E i n - E o u t = m ˙ P, i n × e P, i n + W P - m ˙ P, o u t × e P, o u t$
转化器	$Δ E C o = E i n - E o u t = m ˙ C o, i n × e C o, i n - ∑ i = 1 n m ˙ C o_i, o u t × e C o_i, o u t$

物流	温度/℃	压力/kPa	质量流量/kg·h^-1	质量?/kJ·kg^-1
Feed	25	140	208.3	397.7
GH1	8.8	140	1535.3	404.5
GH2	119.1	388.9	1535.3	1835.1
GH3	25	388.9	1535.3	1654.8
GH4	142.1	1080.1	1535.3	3181.5
GH5	25	1080.1	1535.3	2913.4
GH6	142.3	3000	1535.3	4446.1
GH7	25	3000	1535.3	4176.6
GH8	-91	3000	1535.3	4647.2
GH9	-155.5	3000	1535.3	5688.1
GH10	-189	3000	1535.3	6792.2
GH11	-195.7	2125	1535.3	6641.8
GH12	-214.5	2125	1535.3	7774.6
GH13	-219.4	1500	1535.3	7660.4
GH14	-238.3	1500	1535.3	10345.1
GH15	-252	140	1535.3	9963.2
LH	-251.8	140	208.3	14627
BH1	-251.8	140	1327	8742.2
BH2	-221.5	140	1327	4776.6
BH3	-197.9	140	1327	3337.1
BH4	-157.5	140	1327	1939.7
BH5	-94.4	140	1327	899.7
BH6	6.3	140	1327	406.8
LNG1	-160	120	1120	957.9
LNG2	-158.5	3000	1120	959
LNG3	-94.4	3000	1120	720.3
NG	23	3000	1120	460.1

物流	正氢比例/%	仲氢比例/%
Feed	75	25
GH1	12.21	88.97
BH1	1.19	98.81
LH	0.90	99.10

参数	值
压缩机功耗/kW	2156.65
LNG泵功耗/kW	2.62
膨胀机回收功/kW	117.06
SEC/	9.802
EXE/%	41.4

多流热交换器	最小温差/℃	U/kW·℃^-1
HX1	2	57.35
HX2	2.012	191.13
HX3	2.042	51.66
HX4	2.203	34.80
HX5	2.078	36.54

设备	?损失/kW	?破坏率/%
Com-1	80.47	5.9
Com-2	80.51	5.9
Com-3	80.81	5.9
C-1	76.90	0.2
C-2	114.34	1.8
C-3	114.93	1.7
P-1	2.28	8
E-1	25.30	4.5
E-2	23.59	1
E-3	109.78	3.2
HX1	61.94	3.5
HX2	13.7	23.1
HX3	44.23	5.6
HX4	47.51	8.3
HX5	316.81	8.4
Co-1	180.22	13.1
总计	1373.3	100

氢液化系统	比能耗/	?效率/%
理想预冷Linde-Hampson^［22］	16.27	27
LNG预冷L-H系统	14.30	28.53
Ingolstadt氢气液化流程^［23］	13.58	21
氦制冷液化流程^［24］	10.25	37.98
氮气预冷单压Claude系统^［22］	10	32.6
新型双压L-H系统	9.802	41.4
氮气预冷双压Claude系统^［22］	8.68	37.7
Quack氢气液化系统^［4］	6.93	52.6
WE-NET氢气液化系统^［4］	8.53	41.3

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