考虑延迟特性的电厂-碳捕集系统优化调度

doi:10.11949/0438-1157.20251139

摘要/Abstract

摘要：

为提升电厂-碳捕集系统的运行效能，本研究建立了碳捕集过程的稳态与动态机理模型，通过阶跃响应实验辨识其动态特性及关键输入变量，并将关键响应时间常数作为约束引入调度模型。在此基础上，提出了一种协调调度策略，该策略计及电厂负荷波动与碳捕集系统的动态延迟响应，通过引入储罐、烟气旁路等灵活运行手段，在充分挖掘碳捕集系统调节潜力、提升电厂经济性与实现减排目标的同时，确保了调度方案与各单元动态运行特性的相容性及实际可行性。算例结果表明，相较于传统不考虑延迟的调度策略，本研究提出的方法不仅在日运行成本上略有降低，并且可针对系统动态惯性问题实现前瞻性调度，在第一个用电高峰期及之前时段（1~10h），富液储罐主动储存CO₂的能力提高40.3%，有效避免了储罐液位触及安全运行下限；在第二个用电高峰期及之前时段（18~24h），将前期储存的CO₂主动释放，使同期CO₂产量较传统策略提升93.8%，其全天产量占比由19.68%提高至38.13%，显著的平滑了产品输出波动，保障CO₂产品流量的稳定供应，提升与下游碳利用产业链的协同效率。

关键词: 二氧化碳捕集, 动态建模, 优化调度, 灵活操作, 瞬态响应

Abstract:

To enhance the operational efficiency of power plant carbon capture systems, this study established steady-state and dynamic mechanism models for the carbon capture process. Through step response experiments, dynamic characteristics and key input variables were identified, with critical response time constants incorporated as constraints into the scheduling model. Based on this foundation, a coordinated scheduling strategy was proposed that simultaneously accounts for both power plant load fluctuations and the dynamic delay response of the carbon capture system. By flexibly deploying operational measures such as storage tanks and flue gas bypasses, the model fully unleashes the carbon capture system's regulatory potential. This approach enhances plant economic benefits while achieving emission reduction targets, ensuring scheduling plans remain compatible with the dynamic operational characteristics of each unit and maintain practical feasibility.The calculation results show that compared with traditional scheduling strategies that do not consider delays, the method proposed in this study not only slightly reduces daily operating costs, but also achieves forward-looking scheduling for system dynamic inertia problems. During the first peak electricity consumption period and the preceding period (1~10 hours), the active storage capacity of CO₂ in the rich liquid storage tank is increased by 40.3%, effectively avoiding the tank liquid level from reaching the safe operating lower limit; During the second peak electricity consumption period and before (18~24h), the previously stored CO₂ was actively released, resulting in a 93.8% increase in CO₂ production compared to traditional strategies during the same period. The proportion of daily production increased from 19.68% to 38.13%, significantly smoothing out product output fluctuations, ensuring stable supply of CO₂ product flow, and improving the collaborative efficiency with downstream carbon utilization industry chains.

Key words: CO₂ capture, dynamic modeling, optimal scheduling, flexible operation, transient response

中图分类号:

TQ 021.8

李良君, 张芮萌, 庄钰, 都健, 刘琳琳. 考虑延迟特性的电厂-碳捕集系统优化调度[J]. 化工学报, DOI: 10.11949/0438-1157.20251139.

Liangjun LI, Ruimeng ZHANG, Yu ZHUANG, Jian DU, Linlin LIU. Optimal scheduling of power plant carbon capture system considering delay characteristics[J]. CIESC Journal, DOI: 10.11949/0438-1157.20251139.

图/表 17

图1 基于MEA溶剂吸收法的碳捕集流程图

Fig.1 Flow diagram of carbon capture based on MEA solvent absorption method

表1 吸收/解吸塔中平衡反应方程式

Table 1 Equilibrium reaction equation in absorption/desorption tower

反应类型	化学方程式
还原氨基甲酸盐	$M E A C O O - + H 2 O ↔ M E A + H C O 3 -$
MEA去质子化	$M E A H + + H 2 O ↔ M E A + H 3 O +$
生成碳酸氢盐	$C O 2 + 2 H 2 O ↔ H 3 O + + H C O 3 -$
生成碳酸盐	$H C O 3 - + 2 H 2 O ↔ H 3 O + + C O 3 2 -$
水解离	$2 H 2 O ↔ H 3 O + + O H -$

表1 吸收/解吸塔中平衡反应方程式

Table 1 Equilibrium reaction equation in absorption/desorption tower

反应类型	化学方程式
还原氨基甲酸盐	$M E A C O O - + H 2 O ↔ M E A + H C O 3 -$
MEA去质子化	$M E A H + + H 2 O ↔ M E A + H 3 O +$
生成碳酸氢盐	$C O 2 + 2 H 2 O ↔ H 3 O + + H C O 3 -$
生成碳酸盐	$H C O 3 - + 2 H 2 O ↔ H 3 O + + C O 3 2 -$
水解离	$2 H 2 O ↔ H 3 O + + O H -$

表2 PCC系统的主要设备参数

Table 2 Equipment parameters of PCC system

塔设备	参数	数值
吸收塔	塔高	18 m
	塔径	12 m
	温度（塔釜）	318.5 K
	压力	101.3 kPa
	填料类型	IMTP#50
	填料信息	NORTON-METAL
	填料规格	2-IN OR 50-MM
解吸塔	塔高	18 m
	塔径	10 m
	温度（塔釜）	389 K
	压力	150 kPa
	填料类型	SULZER-STANDARD
	填料信息	MELLAPAK
	填料规格	250Y

表3 PCC系统的主要运行参数

Table 3 Operating parameters of PCC system

主要参数	数值
CO₂捕集率	89%
换热器热负荷	69.7 MW
再沸器热负荷	318.6 MW
冷凝器热负荷	-165.9 MW
富液CO₂负荷	0.538 molCO₂/molMEA
温度（贫液）	313 K
压力	150 kPa
质量流量	660 kg/s
各组分质量分数	0.0618 CO₂
	0.6334 H₂O
	0.3048 MEA
CO₂负荷(解吸后)	0.286 molCO₂/molMEA
温度（烟气）	333 K
压力	110 kPa
质量流量	200 kg/s
组分质量分数^[22]	0.209 CO₂
	0.042 H₂O
	0.748 N₂
	0.001 O₂

图2 多元线性回归模型验证

Fig.2 Verification of multiple linear regression model

图3 烟气流量±10%响应图

Fig.3 Response diagram of flue gas flow ±10%

图4 贫液流量±10%响应图

Fig.4 Response diagram of lean solution flow ±10%

图5 抽汽流量±10%响应图

Fig.5 Response diagram of extraction flow ±10%

图6 添加完整控制回路的动态模型

Fig.6 Dynamic model with complete control loop

表4 日电负荷需求波动

Table.4 Electric load demand fluctuation

时间/h	1	2	3	4	5	6	7	8	9	10	11	12
电负荷/MW	112.5	120.8	127.3	132.3	148.7	161.7	185.3	198.8	191.1	175.1	162.9	151.9

表5 计算结果表

Table.5 Calculation results

相关项目	结果/（USD·day^-1）
相关项目	不考虑延迟的传统调度的电厂	考虑延迟调度的电厂
燃煤成本	374568.16	374193.30
CO₂排放惩罚成本	121946.49	121714.92
购电成本	11707.90	11707.90
操作成本	29617.50	29591.95
日成本	537840.05	537208.09

图7 电厂发电功率调度

Fig.7 Power generation schedule of power plant

图8 储罐中储液量调度

Fig.8 Liquid storage volume schedule in storage tank

图9 CO2吸收/解吸塔负荷调度

Fig.9 CO2 absorption/desorption tower load scheduling

图10 CO2产量调度

Fig.10 CO2 production scheduling

图11 富液储罐不考虑延迟和考虑延迟运行调度比较

Fig.11 Comparison of rich liquid storage tank operation scheduling under different cases

图12 CO2产量不考虑延迟和考虑延迟运行调度比较

Fig.12 Comparison of CO2 production scheduling under different cases

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