基于稳定性分析的含酸/醇烃水体系相平衡计算

doi:10.11949/0438-1157.20231235

化工学报 ›› 2024, Vol. 75 ›› Issue (3): 789-800.DOI: 10.11949/0438-1157.20231235

基于稳定性分析的含酸/醇烃水体系相平衡计算

陈好奇¹(), 史博会¹^,²(), 彭琪¹, 康琦³, 宋尚飞¹, 姚海元⁴, 陈海宏⁴, 吴海浩¹, 宫敬¹

^1.中国石油大学（北京）油气管道输送安全国家工程实验室，石油工程教育部重点实验室，城市油气输配技术北京市重点实验室，北京 102249
^2.中国石油大学（北京）碳中和示范性能源学院，北京 102249
^3.清华大学，深圳清华大学研究院，广东深圳 518057
^4.中海油研究总院有限责任公司，北京 100028

收稿日期:2023-11-28 修回日期:2024-02-07 出版日期:2024-03-25 发布日期:2024-05-11
通讯作者: 史博会
作者简介:陈好奇（1997—），男，博士研究生，1649618546@qq.com
基金资助:
国家重点研发计划项目(2022YFC2806200);北京市自然科学基金面上项目(23C20113)

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

Haoqi CHEN¹(), Bohui SHI¹^,²(), Qi PENG¹, Qi KANG³, Shangfei SONG¹, Haiyuan YAO⁴, Haihong CHEN⁴, Haihao WU¹, Jing GONG¹

^1.National Engineering Research Center of Oil and Gas Pipeline Transportation Safety，MOE Key Laboratory of Petroleum Engineering，Beijing Key Laboratory of Urban Oil and Gas Distribution Technology, China University of Petroleum, Beijing 102249, China
^2.College of Carbon Neutral Energy, China University of Petroleum, Beijing 102249, China
^3.Research Institute of Tsinghua University in Shenzhen, Shenzhen 518057, Guangdong, China
^4.CNOOC Research Institute Co. , Ltd. , Beijing 100028, China

Received:2023-11-28 Revised:2024-02-07 Online:2024-03-25 Published:2024-05-11
Contact: Bohui SHI

摘要/Abstract

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

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

中图分类号:

O 642.4⁺2

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.

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.

图/表 17

图1 基于稳定性分析的多相多组分相平衡计算流程

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

表1 甲醇/水与第二组分所构成二元体系的SRK-HV方程交互作用参数［4］

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

图2 稳定性分析迭代求解流程图

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

图3 稳定性分析结合多相闪蒸模型计算示意图

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

表2 Mixture 2的组分数据［4， 12， 31］

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

表2 Mixture 2的组分数据［4， 12， 31］

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

表3 6.03 MPa、276.75 K下气-油-水相平衡结果对比

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

图4 本文模型与Sabet等[17]的相分率计算结果对比

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

表4 含酸气烃水混合物［17， 31］

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

表4 含酸气烃水混合物［17， 31］

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

图5 27 MPa、300 K下两相闪蒸算法的收敛效果对比

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

图6 4 MPa、460 K下三相闪蒸算法的收敛效果对比

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

表5 含CO2的烃水混合物物性参数［18， 31］

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

表5 含CO2的烃水混合物物性参数［18， 31］

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

表6 不同工况下稳定性分析与闪蒸计算耗时对比

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

表7 H2O/ C3/ nC16混合物组成及参数［4， 19］

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

表7 H2O/ C3/ nC16混合物组成及参数［4， 19］

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

图7 H2O/C3/nC16混合物在6 MPa、473 K下的TPD函数图像

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

表8 6 MPa、473 K下H2O/C3/nC16混合物单相检验结果

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

表9 含酸/醇烃水组分及参数［4， 27， 31］

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

表9 含酸/醇烃水组分及参数［4， 27， 31］

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

图8 含酸/醇烃水组分相态特征

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

参考文献 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.

[1]	周辛梓, 李增辉, 孟现阳, 吴江涛. 低温下高纯空气黏度实验研究[J]. 化工学报, 2024, 75(3): 782-788.
[2]	王林, 江荣鼎, 张春晓, 李修真, 谈莹莹. 含R1234yf混合工质汽液相平衡的混合规则评估与预测研究[J]. 化工学报, 2024, 75(2): 475-483.
[3]	杨欣, 王文, 徐凯, 马凡华. 高压氢气加注过程中温度特征仿真分析[J]. 化工学报, 2023, 74(S1): 280-286.
[4]	常明慧, 王林, 苑佳佳, 曹艺飞. 盐溶液蓄能型热泵循环特性研究[J]. 化工学报, 2023, 74(S1): 329-337.
[5]	张化福, 童莉葛, 张振涛, 杨俊玲, 王立, 张俊浩. 机械蒸汽压缩蒸发技术研究现状与发展趋势[J]. 化工学报, 2023, 74(S1): 8-24.
[6]	胡建波, 刘洪超, 胡齐, 黄美英, 宋先雨, 赵双良. 有机笼跨细胞膜易位行为的分子动力学模拟研究[J]. 化工学报, 2023, 74(9): 3756-3765.
[7]	于旭东, 李琪, 陈念粗, 杜理, 任思颖, 曾英. 三元体系KCl + CaCl₂ + H₂O 298.2、323.2及348.2 K相平衡研究及计算[J]. 化工学报, 2023, 74(8): 3256-3265.
[8]	张曼铮, 肖猛, 闫沛伟, 苗政, 徐进良, 纪献兵. 危废焚烧处理耦合有机朗肯循环系统工质筛选与热力学优化[J]. 化工学报, 2023, 74(8): 3502-3512.
[9]	卫雪岩, 钱勇. 微米级铁粉燃料中低温氧化反应特性及其动力学研究[J]. 化工学报, 2023, 74(6): 2624-2638.
[10]	姚晓宇, 沈俊, 李健, 李振兴, 康慧芳, 唐博, 董学强, 公茂琼. 流体气液临界参数测量方法研究进展[J]. 化工学报, 2023, 74(5): 1847-1861.
[11]	陈科, 杜理, 曾英, 任思颖, 于旭东. 四元体系LiCl+MgCl₂+CaCl₂+H₂O 323.2 K相平衡研究及计算[J]. 化工学报, 2023, 74(5): 1896-1903.
[12]	毛元敬, 杨智, 莫松平, 郭浩, 陈颖, 罗向龙, 陈健勇, 梁颖宗. C₆~C₁₀烷醇的SAFT-VR Mie状态方程参数回归及其热物性研究[J]. 化工学报, 2023, 74(3): 1033-1041.
[13]	高靖博, 孙强, 李青, 王逸伟, 郭绪强. 考虑水合物结构转变的含氢气体水合物相平衡模型[J]. 化工学报, 2023, 74(2): 666-673.
[14]	程文婷, 李杰, 徐丽, 程芳琴, 刘国际. AlCl₃·6H₂O在FeCl₃、CaCl₂、KCl及KCl–FeCl₃溶液中溶解度的实验及预测[J]. 化工学报, 2023, 74(2): 642-652.
[15]	徐思远, 潘冬, 蒋朝辉, 刘少强, 余浩洋. 基于稳态传热分析的高炉炉壁温度场建模方法[J]. 化工学报, 2023, 74(12): 4863-4880.

基于稳定性分析的含酸/醇烃水体系相平衡计算

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

RichHTML

PDF (PC)

可视化

摘要/Abstract

引用本文

使用本文

图/表 17

参考文献 33

相关文章 15

编辑推荐

Metrics

本文评价