常规及创新高压凝液回收流程对比

doi:10.16085/j.issn.1000-6613.2018-1994

摘要/Abstract

摘要：

塔里木盆地地区的英买、迪那等大型高压凝析气田目前仅对原料天然气进行了烃水露点控制，重烃回收率低，经济效益没有实现最大化，对此类气田进行凝液回收可显著提升气田的经济效益。现今适用于高压天然气凝液回收的流程主要为HPA（high pressure absorber）流程，本文在HPA流程基础上提出两种改进流程，即改进Ⅰ型流程和改进Ⅱ型流程。并通过SQP（sequential quadratic programming）算法以单位能耗最低为目标函数对3种流程进行操作参数优化, 并通过能耗分析表明：3种流程具有不同原料气贫富和压力适应范围，在贫气条件下，原料气压力在7000~8000kPa范围内，改进Ⅰ型比HPA流程更节能，而当原料气压力高于7500kPa时，改进Ⅱ型流程能耗开始低于前两者，且随原料气压力增加，节能效果更加明显。而对于富气，改进Ⅱ型流程能耗最高，改进Ⅰ型与HPA流程区别不明显。

关键词: 高压凝液回收, 流程改进, 流程优化, 能耗分析

Abstract:

Large-scale high-pressure condensate gas fields such as Yingmai and Dina in the Tarim Basin area currently only simply control the dew and hydrocarbon point for the feed natural gas. The recovery rate of heavy hydrocarbons is very low and the economic benefits are not maximized. Taking NGL (natural gas liquid) recovery for gas fields can significantly increase the economic benefits of these fields. Nowadays, HPA (high pressure absorber) process is widely used to recovery NGL for high-pressure natural gas. In this paper two improved processes based on HPA process were proposed: revised type Ⅰ process and revised type Ⅱ process. SQP（sequential quadratic programming） algorithm was selected to optimize the operating parameters of the three processes with the lowest unit energy consumption as the objective function. The energy consumption analysis showed that the three processes had different adaptation range of feed gas richness and pressure. Under lean conditions the revised type Ⅰ process was more energy efficient than HPA process in the range of feed gas pressures of 7000—8000kPa. When the feed gas pressure was higher than 7500kPa, the energy consumption of revised type Ⅱ process started to be lower than the former two, and with the increase of feed gas pressure, the energy saving of revised type Ⅱ process was more obvious. For rich gas, revised type Ⅱ process had the highest energy consumption and the difference between revised type Ⅰ process and HPA processes was not apparent.

Key words: high-pressure NGL recovery, process improvement, process optimization, energy consumption analysis

中图分类号:

TE64

蒋洪, 张世坚, 敬加强, 朱聪. 常规及创新高压凝液回收流程对比[J]. 化工进展, 2019, 38(06): 2581-2589.

Hong JIANG, Shijian ZHANG, Jiaqiang JING, Cong ZHU. Comparison of conventional and novel high-pressure NGL recovery processes[J]. Chemical Industry and Engineering Progress, 2019, 38(06): 2581-2589.

图/表 13

参考文献 19

1	扈海莉 . YM凝析气田天然气凝液回收流程模拟与优化[D]. 成都: 西南石油大学，2014.
	HU Haili . Natural gas liquid recovery process simulation and optimization of YM condensate gas field[D]. Chengdu: Southwest Petroleum University，2014.
2	丁玲 . TLM气田天然气深度凝液回收工艺技术研究[D]. 成都: 西南石油大学，2016.
	DING Ling . Study of deep NGL recovery process in TLM gas filed[D]. Chengdu: Southwest Petroleum University, 2016.
3	邓筑井 . YM高压天然气乙烷回收换热网络研究[D]. 成都: 西南石油大学，2014.
	DENG Zhujing . Heat exchanger network study of high-pressure natural gas in YM gas filed[D]. Chengdu: Southwest Petroleum University, 2014.
4	黄思宇,蒋洪,巴玺立,等 .英买天然气处理装置提高丙烷收率工艺改进研究[J].石油与天然气化工, 2015,44(4):1-7.
	HUANG Siyu , JIANG Hong , BA Xili , et al . Process improvement research on enhancing propane recovery in Yingmai natural gas processing device[J]. Chemical Engineering of Oil & Gas, 2015,44(4):1-7.
5	蒋洪,何愈歆,王军 .高压吸收塔工艺回收天然气凝液的模拟分析[J].天然气化工(C1化学与化工), 2011,36(3):7-11.
	JIANG Hong , HE Yuxin , WANG Jun . Simulation analysis of utilizing high pressure absorber process to recover condensate from natural gas[J]. Natural Gas Chemical Industry, 2011，36(3):7-11.
6	FOGLIETTA J H , HADDAD H , MOWREY E R , et al . Cryogenic process utilizing high pressure absorber column: US0157538[P]. 2002-10-31.
7	FOGLIETTA J H , HADDAD H , MOWERY E R , et al . Cryogenic process utilizing high pressure absorber column: US6712880B2[P]. 2004-03-30.
8	MOWREY E R , FOGLIETTA J H . Efficient, high recovery of liquids from natural gas utilizing a high pressure absorber[C]//Proceedings of the Eighty-First Annual Convention. US: Gas Processors Association, 2002.
9	蒋洪, 黄思宇, 朱聪 . 高压天然气的凝液回收方法: CN104807288B[P]. 2017-03-15.
	JIANG Hong , HUANG Siyu , ZHU Cong . A NGL recovery method for high pressure natural gas: CN104807288B[P]. 2017-03-15.
10	张世坚，蒋洪 .直接换热常规流程的改进及分析[J].化工进展,2017,36(10):3648-3656.
	ZHANG Shijian , JIANG Hong . Improvement and analysis of DHX conventional process[J]. Chemical Industry and Engineering Progress, 2017,36(10):3648-3656.
11	黄思宇 . 含CO₂天然气乙烷回收工艺研究[D]. 成都: 西南石油大学,2015.
	HUANG Siyu . Study of ethane recovery process on natural gas with CO₂ [D]. Chengdu: Southwest Petroleum University，2015.
12	GONG J , YANG M , YOU F . A systematic simulation-based process intensification method for shale gas processing and NGLs recovery process systems under uncertain feedstock compositions[J]. Computers & Chemical Engineering, 2017, 105:259-275.
13	GETU M , MAHADZIR S , LONG N V D , et al . Techno-economic analysis of potential natural gas liquid (NGL) recovery processes under variations of feed compositions[J]. Chemical Engineering Research & Design, 2013, 91(7):1272-1283.
14	国家能源局 . 气田地面工程设计节能技术规范: SY/T 6331—2013[S]. 北京:石油工业出版社，2014.
	National Energy Administration . Technical specification for design of energy conservation for gas field surface engineering: SY/T 6331—2013[S]. Beijing: Petroleum Industry Press,2014.
15	MEHRPOOYA M , VATANI A , MOUSAVIAN S M A . Introducing a novel integrated NGL recovery process configuration (with a self-refrigeration system (open-closed cycle)) with minimum energy requirement[J]. Chemical Engineering & Processing Process Intensification, 2010, 49(4):376-388.
16	NAGY, ZOLTAN, ARKADIY S . Mathematical simulation of natural gas condensation processes using the Peng-Robinson equation of state [C]//SPE Annual Technical Conference and Exhibition. US: Society of Petroleum Engineers, 1982.
17	中华人民共和国国家质量监督检验检疫总局, 中国国家标准化管理委员会 . 综合能耗计算通则: GB/T 2589—2008[S]. 北京: 中国标准出版社, 2008.
	General Administration of Quality Supervision, Inspection and Quarantine of the People’s Republic of China, Standardization Administration of the People’s Republic of China . General principles for calculation of the comprehensive energy consumption: GB/T 2589—2008[S]. Beijing: Standards Press of China, 2008.
18	CAO W , LIN W , LU X , et al . Parameter comparison of two small-scale natural gas liquefaction processes in skid-mounted packages[J]. Gryogenics, 2005, 26(8):898-904.
19	LI Y , XU F , GONG C . System optimization of turbo-expander process for natural gas liquid recovery[J]. Chemical Engineering Research & Design, 2017, 124:159-169.

工况	N₂	CO₂	C₁	C₂	C₃	iC₄	nC₄	iC₅	nC₅	C₆	C₇	C₈ ⁺
1	1.0210	0.3504	88.2883	7.4074	1.5015	0.3003	0.3103	0.1301	0.0901	0.1502	0.2002	0.2503
2	0.9164	0.3655	86.3094	7.2607	3.1431	0.6556	0.6097	0.1285	0.0837	0.1163	0.2220	0.1892

工况	N₂	CO₂	C₁	C₂	C₃	iC₄	nC₄	iC₅	nC₅	C₆	C₇	C₈ ⁺
1	1.0210	0.3504	88.2883	7.4074	1.5015	0.3003	0.3103	0.1301	0.0901	0.1502	0.2002	0.2503
2	0.9164	0.3655	86.3094	7.2607	3.1431	0.6556	0.6097	0.1285	0.0837	0.1163	0.2220	0.1892

参数	数值	参数	数值
外输压力要求/kPa	6000	脱乙烷塔第三股进料位置	17
换热器最小接近温差/℃	4	膨胀机等熵效率/%	85^[14]
吸收塔塔顶与塔底压差/kPa	10	压缩机绝热效率/%	75^[15]
吸收塔理论塔盘数	8	导热油进料温度/℃	280
脱乙烷塔塔顶与塔底压差/kPa	20	导热油出料温度/℃	250
脱乙烷塔理论塔盘数	26	物性流体包	Peng Robinson^[16]
脱乙烷塔第二股进料位置	8	凝液回收率要求/%	≥99

参数	数值	参数	数值
外输压力要求/kPa	6000	脱乙烷塔第三股进料位置	17
换热器最小接近温差/℃	4	膨胀机等熵效率/%	85^[14]
吸收塔塔顶与塔底压差/kPa	10	压缩机绝热效率/%	75^[15]
吸收塔理论塔盘数	8	导热油进料温度/℃	280
脱乙烷塔塔顶与塔底压差/kPa	20	导热油出料温度/℃	250
脱乙烷塔理论塔盘数	26	物性流体包	Peng Robinson^[16]
脱乙烷塔第二股进料位置	8	凝液回收率要求/%	≥99

流程	操作变量	变量范围
流程	操作变量	工况1	工况2
HPA	低温分离器温度（T _S1）/℃	-36≤T _S1≤-30	-18≤T _S1≤-23
	TEE-101分流比（S ₁₀₁）	0.75≤S ₁₀₁≤0.82	0.75≤S ₁₀₁≤0.82
	吸收塔塔底凝液换热后进脱乙烷塔温度（T _S4）/℃	-5≤T _S4≤44
	吸收塔塔压（P _T-101）/kPa	4000≤P _T-101≤4700
	脱乙烷塔塔压（P _T-102）/kPa	3000≤P _T-102≤3800
	塔顶压缩机出口压力（P _S5）/kPa	P _S5＝P _T-101+200
改进Ⅰ型	低温分离器温度（T _S1）/℃	-35≤T _S1≤-28	-25≤T _S1≤-20
	TEE-101分流比（S ₁₀₁）	0.55≤S ₁₀₁≤0.6	0.75≤S ₁₀₁≤0.82
	吸收塔塔底凝液换热后进脱乙烷塔温度（T _S4）/℃	-5≤T _S4≤44
	吸收塔塔压（P _T-101）/kPa	4000≤P _T-101≤4700
	脱乙烷塔塔压（P _T-102）/kPa	3000≤P _T-102≤3800
	塔顶压缩机出口压力（P _S2）/kPa	P _S2＝P _T-101+200
改进Ⅱ型	低温分离器温度（T _S1）/℃	-38≤T _S1≤-32	-33≤T _S1≤-27
	TEE-101分流比（S ₁₀₁）	0.55≤S ₁₀₁≤0.65	0.65≤S ₁₀₁≤0.70
	吸收塔塔底凝液换热后进脱乙烷塔温度（T _S4）/℃	-5≤T _S4≤44
	吸收塔塔压（P _T-101）/kPa	4000≤P _T-101≤4700
	脱乙烷塔塔压（P _T-102）/kPa	3000≤P _T-102≤3800
	增压泵出口压力（P _S2）/kPa	P _S2＝P _T-101+50
	塔顶压缩机出口压力（P _S5）/kPa	P _S5＝P _S6