Phase equilibrium calculation of acid/alcohol hydrocarbon and water system based on stability analysis

doi:10.11949/0438-1157.20231235

Abstract

Abstract:

Well flow materials in oil and gas development mostly exist in the form of oil, gas and water miscibility. For sour oil and gas fields, acid gases such as hydrogen sulfide or carbon dioxide are often present. In order to avoid hydrate formation and blockage of pipelines, the injection of the alcohol inhibitor is a common method, which will make the fluid composition more complex, presenting a multiphase mixed flow of acid/alcohol hydrocarbon and water. Accurate calculation of the phase equilibrium of hydrocarbon and water system containing acid/alcohol is the basis of predicting phase behavior, and the key to support the simulation of multiphase transport flow in this complex system. The phase equilibrium calculation of this systems based on the classical cubic equation of state is widely used, but there is the problem of low accuracy in calculating the distribution of oil-water two-phase components. Therefore, a stability testing method suitable for acid/alcohol hydrocarbon and water system is proposed by introducing stability analysis method. With the SRK-HV equation of state and stability analysis, a multi-phase and multi-component flash calculation model for acid/alcohol hydrocarbon and water is established. After multiple perspectives verification, the model proposed in this research has high accuracy and stability.

Key words: phase equilibria, thermodynamics, equation of state, stability analysis, flash calculation

摘要：

油气开发的井流物多以油气水混相形式存在。对于酸性油气田，还常伴有硫化氢或二氧化碳等酸性气体。为了避免水合物生成堵塞管道，加注醇类防冻剂是常用的方法。因而油气田井流物易于呈现含酸、含醇的多相烃水混输状态。含酸/醇烃水体系相平衡的准确计算，是预测其物性特征的基础，也是支持该复杂体系多相混输流动仿真的关键。但目前被广泛应用的基于经典立方型状态方程计算油气水体系相平衡的方法，存在对液烃及水相分布预测准确性不高的问题。为此，引入稳定性分析的方法，构建适用于含酸/醇烃水体系的稳定性检验方式，结合SRK-HV状态方程，建立了耦合稳定性分析的含酸/醇烃水多相多组分相平衡计算模型及算法。经多角度验证，本研究所提模型具有较高的准确性与稳定性。

关键词: 相平衡, 热力学, 状态方程, 稳定性分析, 闪蒸计算

CLC Number:

O 642.4⁺2

Haoqi CHEN, Bohui SHI, Qi PENG, Qi KANG, Shangfei SONG, Haiyuan YAO, Haihong CHEN, Haihao WU, Jing GONG. Phase equilibrium calculation of acid/alcohol hydrocarbon and water system based on stability analysis[J]. CIESC Journal, 2024, 75(3): 789-800.

陈好奇, 史博会, 彭琪, 康琦, 宋尚飞, 姚海元, 陈海宏, 吴海浩, 宫敬. 基于稳定性分析的含酸/醇烃水体系相平衡计算[J]. 化工学报, 2024, 75(3): 789-800.

Figures/Tables 17

Fig.1 Flow chart of multiphase multicomponent phase equilibrium calculation based on stability analysis

Table 1 Interaction parameters for binary mixtures of methanol/water and the indicated second component ［4］

第二组分	甲醇			水
第二组分	[(g₁₂-g₂₂)/R]/K	[(g₂₁-g₁₁)/R]/K	α₁₂	[(g₁₂-g₂₂)/R]/K	[(g₂₁-g₁₁)/R]/K	α₁₂
H₂O	288	276	1.20	—	—	—
N₂	357	1130	0.40	689	3921	0.15
CO₂	247	2970	0.40	16	1652	0.15
H₂S	58	886	0.40	118	1294	0.15
C₁	77	2094	0.40	410	2291	0.15
C₂	255	1610	0.40	492	2281	0.15
C₃	465	1418	0.40	847	2650	0.15
iC₄/nC₄	516	1049	0.40	793	2501	0.15
iC₅	675	1056	0.40	1120	2900	0.15
nC₅	774	1195	0.40	1109	2901	0.15
nC₆	829	1164	0.40	1187	2878	0.15

Fig. 2 Schematic diagram of the iterative solution process for stability analysis

Fig.3 Schematic diagram of stability analysis combined with multiphase flash model calculation

Table 2 Component data of Mixture 2［4， 12， 31］

组分	n_i /%(mol)	p_c_i /MPa	T_c_i /K	ω_i	$k i, N 2$	$k i, C O 2$	$k i, C 1$	$k i, C 2$
N₂	0.64	3.394	126.194	0.040
CO₂	3.10	7.370	304.100	0.239	-0.0315
C₁	72.74	4.641	190.699	0.011	0.0278	0.0960
C₂	8.01	4.884	305.428	0.099	0.0407	0.1400	-0.0089
C₃	4.26	4.257	369.898	0.152	0.0763	0.1370	0.0180	-0.0020
iC₄	0.73	3.648	408.096	0.185	0.0944	0.1370	0.0000	-0.0100
nC₄	1.49	3.797	425.199	0.201	0.0700	0.1410	0.0000	0.0000
iC₅	0.53	3.334	460.398	0.222	0.0867	0.1300	0.0215	0.0000
nC₅	0.64	3.375	469.600	0.254	0.0878	0.1350	0.0000	0.0000
C₆	0.81	3.124	509.108	0.291	0.0800	0.1500	0.0000	0.0000
C₇	1.08	2.875	535.314	0.332	0.0800	0.1500	0.0000	0.0000
C₈	1.20	2.669	556.575	0.368	0.0800	0.1500	0.0000	0.0000
C₉	1.08	2.446	580.830	0.414	0.0800	0.1500	0.0000	0.0000
C₁₀	3.70	2.278	601.487	0.456	0.0800	0.1500	0.0000	0.0000

Table 2 Component data of Mixture 2［4， 12， 31］

组分	n_i /%(mol)	p_c_i /MPa	T_c_i /K	ω_i	$k i, N 2$	$k i, C O 2$	$k i, C 1$	$k i, C 2$
N₂	0.64	3.394	126.194	0.040
CO₂	3.10	7.370	304.100	0.239	-0.0315
C₁	72.74	4.641	190.699	0.011	0.0278	0.0960
C₂	8.01	4.884	305.428	0.099	0.0407	0.1400	-0.0089
C₃	4.26	4.257	369.898	0.152	0.0763	0.1370	0.0180	-0.0020
iC₄	0.73	3.648	408.096	0.185	0.0944	0.1370	0.0000	-0.0100
nC₄	1.49	3.797	425.199	0.201	0.0700	0.1410	0.0000	0.0000
iC₅	0.53	3.334	460.398	0.222	0.0867	0.1300	0.0215	0.0000
nC₅	0.64	3.375	469.600	0.254	0.0878	0.1350	0.0000	0.0000
C₆	0.81	3.124	509.108	0.291	0.0800	0.1500	0.0000	0.0000
C₇	1.08	2.875	535.314	0.332	0.0800	0.1500	0.0000	0.0000
C₈	1.20	2.669	556.575	0.368	0.0800	0.1500	0.0000	0.0000
C₉	1.08	2.446	580.830	0.414	0.0800	0.1500	0.0000	0.0000
C₁₀	3.70	2.278	601.487	0.456	0.0800	0.1500	0.0000	0.0000

Table 3 Comparison of gas-oil-water equilibrium results at 6.03 MPa and 276.75 K

组分	n_i /%(mol)	气相			油相			水相
组分	n_i /%(mol)	x_i,_cal/%(mol)	x_i,_exp/%(mol)	Δx^①/%	x_i,_cal/%(mol)	x_i,_exp/%(mol)	Δx/%	x_i,_cal/%(mol)	x_i,_exp/%(mol)	Δx/%
Mixture 2	84.76	99.946	99.957	-0.01	99.460	99.799	-0.34	—	—	—
甲醇	2.99	0.0426	0.0429	-0.70	0.221	0.201	9.95	18.240	18.680	-2.36
水	7.32	—	—	—	—	—	—	81.410	81.320	0.11

Fig.4 Comparison of the phase fraction calculated results of this model with those of Sabet et al[17]

Table 4 A mixture of acidic gas， hydrocarbon and water［17， 31］

组分	n_i /%(mol)	p_c_i /MPa	T_c_i /K	ω_i	$k i, C O 2$	$k i, n C 5$	$k i, n C 10$
CO₂	42.0	7.370	304.100	0.239
nC₅	3.0	3.375	469.600	0.254	0.1350
nC₁₀	9.0	2.108	617.598	0.488	0.1340	0.0000
H₂S	15.0	9.008	373.600	0.081	0.1150	0.0709	0.0000
H₂O	31.0	22.120	647.299	0.344	0.0000	0.0000	0.5000

Table 4 A mixture of acidic gas， hydrocarbon and water［17， 31］

组分	n_i /%(mol)	p_c_i /MPa	T_c_i /K	ω_i	$k i, C O 2$	$k i, n C 5$	$k i, n C 10$
CO₂	42.0	7.370	304.100	0.239
nC₅	3.0	3.375	469.600	0.254	0.1350
nC₁₀	9.0	2.108	617.598	0.488	0.1340	0.0000
H₂S	15.0	9.008	373.600	0.081	0.1150	0.0709	0.0000
H₂O	31.0	22.120	647.299	0.344	0.0000	0.0000	0.5000

Fig.5 Comparison of convergence effect of two-phase flash algorithm at 27 MPa and 300 K

Fig.6 Comparison of convergence effect of three-phase flash algorithm at 4 MPa and 460 K

Table 5 Component data for hydrocarbon and water mixtures containing CO2 ［18， 31］

组分	p_c_i /MPa	T_c_i /K	ω_i	$k i, C 1$	$k i, C O 2$
C₁	4.641	190.699	0.011
CO₂	7.370	304.100	0.239	0.0960
H₂S	9.008	373.600	0.081	0.0755	0.1150
H₂O	22.120	647.299	0.344	0.0000	0.0000

Table 5 Component data for hydrocarbon and water mixtures containing CO2 ［18， 31］

组分	p_c_i /MPa	T_c_i /K	ω_i	$k i, C 1$	$k i, C O 2$
C₁	4.641	190.699	0.011
CO₂	7.370	304.100	0.239	0.0960
H₂S	9.008	373.600	0.081	0.0755	0.1150
H₂O	22.120	647.299	0.344	0.0000	0.0000

Table 6 Comparison of stability analysis and flash calculation time under different conditions

组分	T/K	p/MPa	n_i^①/%(mol)	计算耗时/ms
				单相检验		两相闪蒸		两相检验		三相闪蒸		闪蒸过程^②
				文献数据	本文模型	文献数据	本文模型	文献数据	本文模型	文献数据	本文模型	文献数据	本文模型
C₁/ CO₂/ H₂S/ H₂O	37.8	7.60	(14.88, 29.91, 4.94, 50.27)	0.211	0.104	0.117	0.208	0.223	0.119			0.551	0.431
	107.2	12.93	(14.96, 30.09, 4.98, 49.97)	0.213	0.119	0.123	0.518	0.197	0.130			0.533	0.767
	176.7	18.17	(4.96, 4.94, 40.00, 50.00)	0.228	0.108	0.192	0.321	0.230	0.178			0.650	0.607
	37.8	6.26	(5.04, 5.03, 39.86, 50.08)	0.272	0.151	0.139	0.400	0.234	0.254	1.980	0.511	2.625	1.316

Table 7 Component data for H2O/ C3/ nC16 mixture ［4， 19］

组分	n_i /%(mol)	p_c_i /MPa	T_c_i /K	ω_i	$k i, H 2 O$
H₂O	75.0	22.120	647.299	0.344
C₃	15.0	4.257	369.898	0.152	0.0
nC₁₆	10.0	1.419	717.000	0.742	0.5

Table 7 Component data for H2O/ C3/ nC16 mixture ［4， 19］

组分	n_i /%(mol)	p_c_i /MPa	T_c_i /K	ω_i	$k i, H 2 O$
H₂O	75.0	22.120	647.299	0.344
C₃	15.0	4.257	369.898	0.152	0.0
nC₁₆	10.0	1.419	717.000	0.742	0.5

Fig.7 TPD function image of H2O/C3/nC16 mixture at 6 MPa and 473 K

Table 8 Single phase stability analysis results of H2O/C3/nC16 mixture at 6 MPa and 473 K

试验相假设条件

y_i /%(mol)

{H₂O, C₃, nC₁₆}

{99.99, 4.29×10^-3, 3.80×10^-22}

-0.92

否

Table 9 Component data for acid/alcohol hydrocarbon and water mixtures ［4， 27， 31］

组分	n_i /%(mol)	p_c_i /MPa	T_c_i /K	ω_i	$k i, H 2 O$	$k i, N 2$	$k i, C O 2$	$k i, C 1$	$k i, C 2$
H₂O	0.302	22.120	647.299	0.344
MeOH	0.042	8.097	512.640	0.565	0.0000
N₂	0.385	3.394	126.194	0.040	0.0000
CO₂	3.268	7.370	304.100	0.239	0.0000	-0.0315
C₁	86.249	4.641	190.699	0.011	0.0000	0.0278	0.0960
C₂	5.486	4.884	305.428	0.099	0.0000	0.0407	0.1400	-0.0089
C₃	2.061	4.257	369.898	0.152	0.0000	0.0763	0.1370	0.0180	-0.0020
iC₄	0.396	3.648	408.096	0.185	0.0000	0.0944	0.1370	0.0000	-0.0100
nC₄	0.520	3.797	425.199	0.201	0.0000	0.0700	0.1410	0.0215	0.0000
iC₅	0.239	3.334	460.398	0.222	0.0000	0.0867	0.1300	0.0000	0.0000
nC₅	0.177	3.375	469.600	0.254	0.0000	0.0878	0.1350	0.0000	0.0000
nC₆	0.208	3.025	507.600	0.300	0.0000	0.1650	0.1420	0.0000	0.0000
nC₇	0.291	2.740	540.200	0.350	0.5000	0.0800	0.1090	0.0000	0.0000
nC₈	0.208	2.490	568.700	0.399	0.5000	0.0800	0.1350	0.0000	0.0000
nC₉	0.104	2.290	594.600	0.445	0.5000	0.0800	0.1350	0.0000	0.0000
nC₁₀	0.062	2.108	617.598	0.488	0.5000	0.1280	0.1340	0.0000	0.0000

Table 9 Component data for acid/alcohol hydrocarbon and water mixtures ［4， 27， 31］

组分	n_i /%(mol)	p_c_i /MPa	T_c_i /K	ω_i	$k i, H 2 O$	$k i, N 2$	$k i, C O 2$	$k i, C 1$	$k i, C 2$
H₂O	0.302	22.120	647.299	0.344
MeOH	0.042	8.097	512.640	0.565	0.0000
N₂	0.385	3.394	126.194	0.040	0.0000
CO₂	3.268	7.370	304.100	0.239	0.0000	-0.0315
C₁	86.249	4.641	190.699	0.011	0.0000	0.0278	0.0960
C₂	5.486	4.884	305.428	0.099	0.0000	0.0407	0.1400	-0.0089
C₃	2.061	4.257	369.898	0.152	0.0000	0.0763	0.1370	0.0180	-0.0020
iC₄	0.396	3.648	408.096	0.185	0.0000	0.0944	0.1370	0.0000	-0.0100
nC₄	0.520	3.797	425.199	0.201	0.0000	0.0700	0.1410	0.0215	0.0000
iC₅	0.239	3.334	460.398	0.222	0.0000	0.0867	0.1300	0.0000	0.0000
nC₅	0.177	3.375	469.600	0.254	0.0000	0.0878	0.1350	0.0000	0.0000
nC₆	0.208	3.025	507.600	0.300	0.0000	0.1650	0.1420	0.0000	0.0000
nC₇	0.291	2.740	540.200	0.350	0.5000	0.0800	0.1090	0.0000	0.0000
nC₈	0.208	2.490	568.700	0.399	0.5000	0.0800	0.1350	0.0000	0.0000
nC₉	0.104	2.290	594.600	0.445	0.5000	0.0800	0.1350	0.0000	0.0000
nC₁₀	0.062	2.108	617.598	0.488	0.5000	0.1280	0.1340	0.0000	0.0000

Fig.8 Phase behavior of acid/alcohol hydrocarbon and water mixtures

References 33

1	迟东辉. 油田伴生气酸性气体脱除技术研究[D]. 大庆: 大庆石油学院, 2007.
	Chi D H. Study on removing acid gas from associated gas in oil field[D]. Daqing: Daqing Petroleum Institute, 2007.
2	张衍壮, 韩莎莎, 孙晓岩, 等. 汽-液-游离水三相闪蒸模型研究与开发[J]. 昆明理工大学学报(自然科学版), 2017, 42(6): 92-99.
	Zhang Y Z, Han S S, Sun X Y, et al. Research and development of three-phase vapor-liquid-free-water flash model[J]. Journal of Kunming University of Science and Technology (Natural Science Edition), 2017,42(6): 92-99.
3	Lapene A, Nichita D V, Debenest G, et al. Three-phase free-water flash calculations using a new modified Rachford-Rice equation[J]. Fluid Phase Equilibria, 2010, 297(1): 121-128.
4	Pedersen K S, Christensen P L, Shaikh J A, et al. Phase Behavior of Petroleum Reservoir Fluids[M]. Florida: CRC Press, 2006.
5	高冉. 油藏多相多组分相平衡实验及计算方法研究[D]. 北京: 中国地质大学(北京), 2018.
	Gao R. Multiphase and multi-component phase equilibrium experiment and calculation research for oil reservoir[D]. Beijing: China University of Geosciences, 2018.
6	Kabadi V N, Danner R P. A modified Soave-Redlich-Kwong equation of state for water-hydrocarbon phase equilibria[J]. Industrial & Engineering Chemistry Process Design and Development, 1985, 24(3): 537-541.
7	Silva G M, Abreu C R A, Tavares F W. Renormalization group theory applied to the CPA equation of state: impacts on phase equilibrium and derivative properties[J]. Fluid Phase Equilibria, 2020, 506: 112365.
8	Monteiro M F, Moura-Neto M H, Pereira C G, et al. Description of phase equilibrium and volumetric properties for CO₂+water and CO₂+ethanol using the CPA equation of state[J]. The Journal of Supercritical Fluids, 2020,161: 104841.
9	Folas G K, Kontogeorgis G M, Michelsen M L, et al. Application of the cubic-plus-association (CPA) equation of state to complex mixtures with aromatic hydrocarbons[J]. Industrial & Engineering Chemistry Research, 2006, 45(4): 1527-1538.
10	Kontogeorgis G M, Folas G K. Thermodynamic Models for Industrial Applications: from Classical and Advanced Mixing Rules to Association Theories[M]. Hoboken: John Wiley & Sons, 2009.
11	Huron M J, Vidal J. New mixing rules in simple equations of state for representing vapour-liquid equilibria of strongly non-ideal mixtures[J]. Fluid Phase Equilibria, 1979, 3(4): 255-271.
12	Pedersen K S, Michelsen M L, Fredheim A O. Phase equilibrium calculations for unprocessed well streams containing hydrate inhibitors[J]. Fluid Phase Equilibria, 1996, 126(1): 13-28.
13	Pedersen K S, Milter J, Rasmussen C P. Mutual solubility of water and a reservoir fluid at high temperatures and pressures[J]. Fluid Phase Equilibria, 2001, 189(1/2): 85-97.
14	Nelson P A. Rapid phase determination in multiple-phase flash calculations[J]. Computers & Chemical Engineering, 1987, 11(6):581-591.
15	Michelsen M L. The isothermal flash problem (Part Ⅰ): Stability[J]. Fluid Phase Equilibria, 1982, 9(1): 1-19.
16	Michelsen M L. The isothermal flash problem (Part Ⅱ): Phase-split calculation[J]. Fluid Phase Equilibria, 1982, 9(1): 21-40.
17	Sabet N, Gahrooei H R E. A new robust stability algorithm for three phase flash calculations in presence of water[J]. Journal of Natural Gas Science and Engineering, 2016, 35: 382-391.
18	Li Z D, Firoozabadi A. General strategy for stability testing and phase-split calculation in two and three phases[J]. SPE Journal, 2012, 17(4): 1096-1107.
19	Li R X, Li H A. Improved three-phase equilibrium calculation algorithm for water/hydrocarbon mixtures[J]. Fuel, 2019, 244: 517-527.
20	Rachford H H, Rice J D. Procedure for use of electronic digital computers in calculating flash vaporization hydrocarbon equilibrium[J]. Journal of Petroleum Technology, 1952, 4(10): 13-19.
21	Leibovici C F, Neoschil J. A solution of Rachford-Rice equations for multiphase systems[J]. Fluid Phase Equilibria, 1995,112(2): 217-221.
22	Okuno R, Johns R T T, Sepehrnoori K. A new algorithm for rachford-rice for multiphase compositional simulation[J]. SPE Journal, 2010, 15(2): 313-325.
23	Qiu L, Wang Y, Jiao Q, et al. Development of a thermodynamically consistent, robust and efficient phase equilibrium solver and its validations[J]. Fuel, 2014, 115: 1-16.
24	Achour S H, Okuno R. Two-phase flash for tight porous media by minimization of the Helmholtz free energy[J]. Fluid Phase Equilibria, 2021, 534: 112960.
25	敬洪彬. 含CO₂油气烃体系多相闪蒸计算模型研究[D]. 北京: 中国石油大学(北京), 2020.
	Jing H B. Multiphase equilibrium modeling for CO₂-hydrocarbon system[D]. Beijing: China University of Petroleum, 2020.
26	Soave G. Equilibrium constants from a modified Redlich-Kwong equation of state[J]. Chemical Engineering Science, 1972, 27(6): 1197-1203.
27	Whitson C H, Brulé M R. Phase Behavior[M]. Richardson, Tex: Henry L. Doherty Memorial Fund of AIME, Society of Petroleum Engineers, 2000.
28	李靖. 高温高压高含CO₂天然气在地层水中溶解度理论研究[D]. 成都: 西南石油大学, 2017.
	Li J. Theoretical study on solubility of high CO₂ content natural gas in formation water at high temperature and high pressure[D]. Chengdu: Southwest Petroleum University, 2017.
29	Perschke D R. Equation of state phase behavior modeling for compositional simulation[D]. Texas: The University of Texas at Austin, 1988.
30	Pasad G V, Venkatarathnam G. A method for avoiding trivial roots in isothermal flash calculations using cubic equations of state[J]. Industrial & Engineering Chemistry Research, 1999, 38(9): 3530-3534.
31	Knapp H, Döring R, Oellrich L, et al. Vapor-Liquid Equilibria for Mixtures of Low-Boiling Substances DECHEMA Chemistry Data Series[M]. Frankfurt/Main, F. R. Germany: Schon, Wetzel GmbH, 1981.
32	Li Y K, Nghiem L X. Phase equilibria of oil, gas and water/brine mixtures from a cubic equation of state and Henry's law[J]. The Canadian Journal of Chemical Engineering, 1986, 64(3): 486-496.
33	Peng D Y, Robinson D B. Two and three phase equilibrium calculations for systems containing water[J]. The Canadian Journal of Chemical Engineering, 1976, 54(6): 595-599.

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[3]	Minghui CHANG, Lin WANG, Jiajia YUAN, Yifei CAO. Study on the cycle performance of salt solution-storage-based heat pump [J]. CIESC Journal, 2023, 74(S1): 329-337.
[4]	Jianbo HU, Hongchao LIU, Qi HU, Meiying HUANG, Xianyu SONG, Shuangliang ZHAO. Molecular dynamics simulation insight into translocation behavior of organic cage across the cellular membrane [J]. CIESC Journal, 2023, 74(9): 3756-3765.
[5]	Xudong YU, Qi LI, Niancu CHEN, Li DU, Siying REN, Ying ZENG. Phase equilibria and calculation of aqueous ternary system KCl + CaCl₂ + H₂O at 298.2, 323.2, and 348.2 K [J]. CIESC Journal, 2023, 74(8): 3256-3265.
[6]	Manzheng ZHANG, Meng XIAO, Peiwei YAN, Zheng MIAO, Jinliang XU, Xianbing JI. Working fluid screening and thermodynamic optimization of hazardous waste incineration coupled organic Rankine cycle system [J]. CIESC Journal, 2023, 74(8): 3502-3512.
[7]	Xueyan WEI, Yong QIAN. Experimental study on the low to medium temperature oxidation characteristics and kinetics of micro-size iron powder [J]. CIESC Journal, 2023, 74(6): 2624-2638.
[8]	Ke CHEN, Li DU, Ying ZENG, Siying REN, Xudong YU. Phase equilibria and calculation of quaternary system LiCl+MgCl₂+CaCl₂+H₂O at 323.2 K [J]. CIESC Journal, 2023, 74(5): 1896-1903.
[9]	Yuanjing MAO, Zhi YANG, Songping MO, Hao GUO, Ying CHEN, Xianglong LUO, Jianyong CHEN, Yingzong LIANG. Estimation of SAFT-VR Mie equation of state parameters and thermodynamic properties of C₆—C₁₀ alcohols [J]. CIESC Journal, 2023, 74(3): 1033-1041.
[10]	Jingbo GAO, Qiang SUN, Qing LI, Yiwei WANG, Xuqiang GUO. Hydrate equilibrium model of hydrogen-containing gas considering hydrates structure transformation [J]. CIESC Journal, 2023, 74(2): 666-673.
[11]	Siyuan XU, Dong PAN, Zhaohui JIANG, Shaoqiang LIU, Haoyang YU. Modeling method of blast furnace wall temperature field based on steady-state heat transfer analysis [J]. CIESC Journal, 2023, 74(12): 4863-4880.
[12]	Junrui DENG, Zeyu LI, Jiayan CHEN. Pseudo-passive heat removal system for thermal safety of power battery [J]. CIESC Journal, 2023, 74(11): 4679-4687.
[13]	Fang ZHOU, Jian LIU, Xiaosong ZHANG. Selection of ternary zeotropic mixtures for high-temperature heat pumps on multiparameter evaluation principles [J]. CIESC Journal, 2023, 74(11): 4487-4500.
[14]	Jin CAI, Xiaohui WANG, Han TANG, Guangjin CHEN, Changyu SUN. Prediction of the phase equilibrium of semi-clathrate hydrate in TBAB aqueous solution [J]. CIESC Journal, 2023, 74(1): 408-415.
[15]	Huan ZHOU, Mengli ZHANG, Qing HAO, Si WU, Jie LI, Cunbing XU. Process mechanism and dynamic behaviors of magnesium sulfate type carnallite converting into kainite [J]. CIESC Journal, 2022, 73(9): 3841-3850.