基于夹点技术考虑含有复杂相变及碳排放的换热网络综合

郑鑫; 李鼎昊; 毛凯田; 展益彬; 王璟德; 孙巍

doi:10.14135/j.cnki.1006-3080.20220107004

基于夹点技术考虑含有复杂相变及碳排放的换热网络综合

doi: 10.14135/j.cnki.1006-3080.20220107004

1.
北京化工大学化学工程学院, 北京 100029
2.
上海卓然工程技术股份有限公司, 上海 200050
3.
上海卓然数智能源有限公司, 上海 200335

详细信息

作者简介:
郑鑫（1997—），女，山西人，硕士生，主要研究方向：过程系统工程，E-mail：2020200069@mail.buct.edu.cn

通讯作者:
王璟德，jingdewang@mail.buct.edu.cn,

中图分类号: TQ021.8
计量
- 文章访问数: 28
- HTML全文浏览量: 30
- PDF下载量: 6
- 被引次数: 0
出版历程
- 收稿日期: 2022-01-07
- 网络出版日期: 2022-05-12

Heat Exchanger Network Synthesis with Complex Phase Changes under the Consideration of Carbon Emissions based on Pinch Point Method

1.
College of Chemical Engineering, Beijing University of Chemical Technology, Beijing 100029, China
2.
Shanghai SupeZET Engineering Technology Co. Ltd, Shanghai 200050, China
3.
Shanghai SuepZET Data Intelligence Energy Co. Ltd, Shanghai 200335, China

摘要

摘要: 以某乙烯裂解工艺中6股用公用工程换热的物流为对象，存在混合物的复杂相变的物流，根据其热负荷和物料特性把相变段折算成一股或多股恒定热容流率的物流，确定温度区间，再用问题表确定夹点。传统夹点法确定最小传热温差△T_min为11℃，加入碳排放目标函数后确定△T_min为9℃，夹点热物流温度为88.3℃，冷物流温度为79.3℃，此时该换热网络所需的最小热公用工程为12727.27 kW，最小冷公用工程为38719.59 kW。根据夹点技术的设计原则和物流匹配准则，可得到能量最优的换热网络结构。
- 换热网络 /
- 夹点技术 /
- 相变 /
- 碳排放 /
- 优化
Abstract: Heat exchanger network, HEN, is one of the most important parts in chemical production process. HEN optimization become an effective tool to save energy and keep sustainable development. There are many methods to optimize HEN. In principle, mathematical programming seems a comprehensive solution, while the pinch point method is still a handy tool, due to its simplicity and clear physical meaning. Special arrangement is required when phase change is considered in the system. The aim of this paper is to investigate six streams distributed in adjacent sections in an ethylene cracking process from systematic perspective, as no heat recovery is involved, and only utility is matched to meet their temperature requirement in process. Problem table is used to determine the pinch point for the design of HEN. Due to the complex phase change of the mixture in the heat exchange system, the phase change section is converted into one or more streams with constant heat capacity flow rate according to its thermal load and material characteristics, so as to determine the temperature interval. In traditional pinch point method, △T_min is found as 11℃, and it is determined to be 9℃ with the consideration of carbon emission. The pinch point is determined by problem table at 88.3℃ for the hot stream and 79.3℃ for the cold stream. Under this condition, the minimum thermal utility required by the heat exchanger network is 12727.27 kW, and the required minimum cold utility is 38719.59kW. The total annual cost is reduced by 2620585.49 USD/a, and the carbon emission is reduced by 61453.50t/a. According to the design principles of pinch technology and stream matching criteria, the energy-efficient heat exchanger network structure has been obtained.
- heat exchanger network /
- pinch technology /
- phase change /
- carbon emission /
- optimization

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图 1 H1温焓图

Figure 1. Temperature-enthalpy diagram for stream H1

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图 2 显示夹点的复合曲线

Figure 2. Composite curves with pinch

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图 3 温度区间图

Figure 3. Temperature interval chart

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图 4 随△T_min变化的不同费用函数

Figure 4. Costs change vs △T_min

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图 5 传统夹点法年度总费用与△T_min关系图

Figure 5. Total annual cost vs. △T_min

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图 6 含碳排放目标年度总费用与△T_min关系图

Figure 6. Total annual cost with the consideration of carbon emission

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图 7 能量最优换热网络

Figure 7. Synthesis of Heat Exchanger Network in terms with utility cost

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表 1 H1流股信息表

Table 1. Information Sheet for stream H1

Stream label	T_in/℃	T_out/℃	Heat capacity flow rate/(kW·℃⁻¹)
H1	88.2	50.9	293.82
H1	50.9	38.0	639.28

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表 2 其余物流信息表

Table 2. Information table for other streams

Stream label	T_in/℃	T_out/℃	Heat capacity flow rate/(kW·℃⁻¹)
H2	88.4	53.0	292.57
H2	53.0	38.0	503.88
H3	88.3	57.4	294.80
H3	57.4	38.0	456.11
C1	42.8	120.1	312.66
C2	37.9	50.0	276.57
C3	37.5	51.4	115.20

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表 3 问题表

Table 3. Problem table

SN	D_K	The outside hot source input the quantity of heat
	D_K	No		Yes
	/kW	I_K/kW	O_K/kW	I_K/kW	O_K/kW
SN1	12756.53	0	−12756.53	12756.53	0
SN2	−15776.81	−12756.53	3020.28	0	15776.81
SN3	−719.94	3020.28	3740.22	15776.81	16496.75
SN4	−316.62	3740.22	4056.84	16496.75	16813.37
SN5	−1301.57	4056.84	5358.41	16813.37	18114.94
SN6	−1199.31	5358.41	6557.72	18114.94	19314.25
SN7	−5491.69	6557.72	12049.41	19314.25	24805.94
SN8	−13916.65	12049.41	25963.06	24805.94	38719.59

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表 4 不同△T_min下结果信息表

Table 4. Cost saving achieved by heat integration under different $\varDelta T_{\rm{{min}}}$

△Tmin/℃	Pinch/℃	Hot Utility/kW	Cold Utility/kW	Energy saving potential
△Tmin/℃	Pinch/℃	Hot Utility/kW	Cold Utility/kW	Hot utility	Cold utility
5	85.8	11476.63	37439.47	60.58%	32.03%
6	85.3	11818.50	37642.23	59.41%	31.66%
7	84.8	12131.20	37943.37	58.33%	31.11%
8	84.3	12414.61	38377.82	57.37%	30.33%
9	83.8	12727.27	38719.59	56.29%	29.71%
10	83.3	13039.93	39002.77	55.22%	29.19%
11	82.8	13381.85	39312.03	54.05%	28.63%
12	82.3	13694.51	39506.67	52.98%	28.28%
13	81.8	14007.17	39750.24	51.81%	27.84%
14	81.3	14319.83	40558.70	50.83%	26.38%

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表 5 费用相关参数表

Table 5. Cost-related parameters

Parameters	Heat exchanger unit area cost CA/USD·a⁻¹	Unit hot utility cost C_HU/USD·kW⁻¹·a⁻¹	Unit cold utility cost C_CU/USD·kW⁻¹·a⁻¹	Heat transfer coefficient between process steams K_HC/W·m⁻²·K⁻¹	Heat transfer coefficient between hot utilities and streams K_HU/W·m⁻²·K⁻¹	Heat transfer coefficient between cold utilities and streams K_CU/W*m-2·K⁻¹
Value	60	100	15	250	540	400

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表 6 费用表

Table 6. Cost details

△T_min/℃	Investment costs/（USD·a⁻¹）	Utilities costs/（USD·a⁻¹）	Total annual cost/（USD·a⁻¹）
5	1196046.86	1709255.09	2905301.95
6	1046183.21	1746483.48	2792666.694
7	939406.52	1782270.58	2721677.099
8	859665.82	1817128.39	2676794.21
9	798614.79	1853520.89	2652135.68
10	750618.90	1889034.59	2639653.49
11	711523.79	1927865.59	2639389.27
12	679833.45	1962051.08	2641884.53
13	653313.02	1996970.60	2650283.62
14	631144.59	2040363.56	2671508.15

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表 7 碳排放费用参数表

Table 7. Parameters in cost calculation for carbon emission

Parameters	NHV/kJ·kg⁻¹	C%	η_Boiler/%	Carbon tax/USD·t⁻¹
Value	30000	74.5	70	20

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表 8 含碳排放费用表

Table 8. Cost with the consideration of carbon Emission

△T_min/℃	Carbon emission/（t·a⁻¹）	Carbon tax cost/（USD·a⁻¹）	Cost with the consideration of carbon Emission/（USD·a⁻¹）
5	43033.82	860676.50	3765978.45
6	44315.73	886314.56	3678981.26
7	45488.26	909765.13	3631442.23
8	46550.96	931019.21	3607813.42
9	47723.34	954466.78	3606602.46
10	48895.72	977914.35	3617567.84
11	50177.81	1003556.16	3642945.43
12	51350.19	1027003.74	3668888.26
13	52522.57	1050451.31	3700734.93
14	53694.94	1073898.88	3745407.02

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