为中间介质气化器（IFV）在多种工作条件下的性能模拟

doi:10.1007/s11708-020-0681-4

Frontiers in Energy

2020, Vol. 14

Issue (3): 452-462 https://doi.org/10.1007/s11708-020-0681-4

研究论文

本期目录

为中间介质气化器（IFV）在多种工作条件下的性能模拟

王博杰¹, 王文¹(

), 齐超¹, 匡以武¹, 许佳伟²

¹. 上海交通大学
². 中海油气电集团技术研发中心

Simulation of performance of intermediate fluid vaporizer under wide operation conditions

Bojie WANG¹, Wen WANG¹(

), Chao QI¹, Yiwu KUANG¹, Jiawei XU²

¹. Institute of Refrigeration and Cryogenics, Shanghai Jiao Tong University, Shanghai 200240, China
². CNOOC Gas and Power Group, Beijing 100027, China

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摘要:

液化天然气因其高效、清洁、安全等优点在能源石油化工工业中广泛应用，在运输和储存中有较多优势的液化天然气在使用中需要进行气化处理，中间介质气化器由于其结构紧凑、水质要求低、不结冰等优势属于LNG接收站主要气化设备之一。中间介质气化器由三个管壳式换热器组成，分别为冷凝器、蒸发器以及调温器。冷凝器与蒸发器共用一个壳层，LNG与海水通过壳层里的中间介质间接换热，中间介质可以是丙烷、乙二醇、丙烯等。论文作者建立了一维分布参数模型，对各种工况下的IFV性能进行了研究，对额定工况的研究中，完成了一部分尺寸参数的优化。对极端工况的研究中，阐述了IFV的局限性，并给出了应对策略；此外，作者还讨论了调温器在IFV中的重要性，以及缺少调温器的IFV在一些特殊极端条件中的应用。

Abstract：

The intermediate fluid vaporizer (IFV) is a typical vaporizer of liquefied natural gas (LNG), which in general consists of three shell-and-tube heat exchangers (an evaporator, a condenser, and a thermolator). LNG is heated by seawater and the intermediate fluid in these heat exchangers. A one-dimensional heat transfer model for IFV is established in this paper in order to investigate the influences of structure and operation parameters on the heat transfer performance. In the rated condition, it is suggested to reduce tube diameters appropriately to get a large total heat transfer coefficient and increase the tube number to ensure the sufficient heat transfer area. According to simulation results, although the IFV capacity is much larger than the simplified-IFV (SIFV) capacity, the mode of SIFV could be recommended in some low-load cases as well. In some cases at high loads exceeding the capacity of a single IFV, it is better to add an AAV or an SCV operating to the IFV than just to increase the mass flow rate of seawater in the IFV in LNG receiving terminals.

Key words： liquefied natural gas intermediate fluid vapo-rizer heat transfer performance numerical simulation extreme condition

收稿日期: 2019-07-24 出版日期: 2020-09-14

通讯作者: 王文 E-mail: wenwang@sjtu.edu.cn

Corresponding Author(s): Wen WANG

引用本文:

王博杰, 王文, 齐超, 匡以武, 许佳伟. 为中间介质气化器（IFV）在多种工作条件下的性能模拟[J]. Frontiers in Energy, 2020, 14(3): 452-462.
Bojie WANG, Wen WANG, Chao QI, Yiwu KUANG, Jiawei XU. Simulation of performance of intermediate fluid vaporizer under wide operation conditions. Front. Energy, 2020, 14(3): 452-462.

链接本文:

https://academic.hep.com.cn/fie/CN/10.1007/s11708-020-0681-4
https://academic.hep.com.cn/fie/CN/Y2020/V14/I3/452

Fig.1

Fig.2

Fig.3

Heat exchanger	Zone	Correlations	Ref.
Evaporator	Inside tube	$Nu = 0.023 Re 0.8 Pr 0.3$	[¹⁷]
Evaporator	Outside tube	$h = 90 q 0.67 M − 0.5 P r n (− lg Pr) − 0.55$	[¹⁸]
Condenser	Inside tube	$Nu = 0.0156 Re 0.82 Pr 0.5 (ρ w ρ b) 0.3 (c ¯ p c pb) n$ $n = {0.4, for ? T b < T w < T pc ? and ? for ? 1.2 T pc < T b < T w 0.4 + 0.2 (T w T pc − 1), for ? T b < T pc < T w 0.4 + 0.2 (T w T pc − 1) [1 − 5 (T b T pc − 1)], for ? T pc < T b < 1.2 T pc ? and ? T b < T w$ $c ¯ p = ∫ T b T w d T / (T w − T b) = (h w − h b) / (T w − T b)$	[¹⁵]
Condenser	Outside tube	$h = 0.79 [G ρ l (ρ l − ρ g) λ 3 r μ l D (T po − T W)] 0.25 ? N eff − 1 / 6$	[¹⁶,¹⁹]
Thermolator	Inside tube	$Nu = 0.023 Re 0.8 Pr 0.3$	[¹⁷]
Thermolator	Outside tube	$Nu f = {1.04 Re f 0.4 Pr f 0.36 (Pr f / Pr w) 0.25, 1 < Re < 5 × 102 0.71 Re f 0.5 Pr f 0.36 (Pr f / Pr w) 0.25, 5 × 102 < Re < 103 0.35 (s 1 s 2) 0.2 Re f 0.6 Pr f 0.36 (Pr f / Pr w) 0.25, s 1 s 2 ≤ 2, 103 < Re < 2 × 105 0.4 Re f 0.6 Pr f 0 .36 (Pr f / Pr w) 0.25, s 1 s 2 > 2, 103 < Re < 2 × 105 ? 0.031 (s 1 s 2) 0.2 Re f 0.8 Pr f 0 .36 (Pr f / Pr w) 0.25, 2 × 105 < Re < 2 × 106$	[²⁰]

Tab.1

Tab.2

Fig.4

Fig.5

Fig.6

Tab.3

T_L1/K	P_L/MPa	$m ˙ L / (t·h – 1)$	T_S1/K	P_S/Mpa	$m ˙ S / (t·h – 1)$
113.15	6	180	281.15	0.2	8750

Tab.4

Fig.7

Fig.8

Fig.9

Fig.10

Fig.11

Fig.12

Fig.13

Fig.14

Tab.5

Fig.15

Fig.16

T	Temperature/K
P	Pressure/MPa
$m ˙$	Mass flow rate/(kg·s^–1)
ρ	Density/(kg·m^–3)
c	Specific heat capacity/(kJ·kg^–1·K^–1)
λ	Thermal conductivity/(W·m^–1·K^–1)
μ	Dynamic viscosity/(Pa·s)
Re	Reynolds number
Pr	Prandtl number
Nu	Nusselt number
G	Gravitational acceleration/(m·s^–2)
$Q ˙$	Heat flux/W
H	Enthalpy/(J·kg^–1)
α	Heat transfer coefficient/(W·m^–2·K^–1)
A	Area/m²
q	Heat flux/(W·m^–2)
r	Heat of vaporization(J·kg^–1)
c_p	Heat capacity/(J·kg^–1·K)
c_pb	Average heat capacity/(J·kg^–1·K)
M	Mass flow rate/(kg·s^–1)
n	Constant
s₁	Horizontal distance between neighboring tubes/m
s₂	Vertical distance between neighboring tubes/m
D	Diameter/m
Subscript
L	LNG or NG
S	Seawater
po	Propane
th	Thermolator
ev	Evaporator
con	Condenser
in	Based on the inside tube
out	Based on the outside tube
w	Based on the tube wall
p	Constant pressure
l	Based on saturated liquid
g	Based on saturated vapor
f	Based on fluid
b	Average value
pc	Pseudo-critical value
eff	Effective

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