基于实际冷、热复合曲线的制苯和碳八装置热联合研究

李振东; 张丹; 杨敏博; 冯霄

doi:10.14135/j.cnki.1006-3080.20220107003

基于实际冷、热复合曲线的制苯和碳八装置热联合研究

doi: 10.14135/j.cnki.1006-3080.20220107003

西安交通大学化学工程与技术学院, 西安 710049

基金项目: 国家自然科学基金资助项目（21736008）

详细信息

作者简介:
李振东（1996—），男，安徽巢湖人，硕士生，研究方向为系统工程

通讯作者:
杨敏博，E-mail：yangmb@xjtu.edu.cn

中图分类号: TQ021.8
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- 文章访问数: 5
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- 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 Integration Scheme for Benzene Production and C₈ Units Based on Actual Cold and Hot Composite Curves

School of Chemical Engineering and Technology, Xi’an Jiaotong University, Xi’an 710049, China

摘要

摘要: 不同装置间的热联合是炼厂提高能量利用率的有效措施。为获得热联合的实际节能潜力和提高改造方案的抗波动能力，提出了基于实际冷、热复合曲线的热联合改造方法。基于某石化企业中制苯装置和碳八装置的工业数据，使用Aspen HYSYS 建立了换热网络模型，并利用Aspen Energy Analyzer进行换热网络分析，提出了制苯装置的换热网络改造方案。通过所提出的改造方法，给出了装置间热联合的节能潜力，并综合改造实施的限制和复杂程度，提出了两个热联合方案，并对方案结果进行了对比和讨论。结果表明，节能较多的方案需要更多的投资成本，投资回收期略长，但从长远来看经济效益更好。
- 实际复合曲线 /
- 热联合 /
- 夹点分析 /
- 节能
Abstract: Heat integration across different units is an effective measure to improve energy utilization in chemical plants. In order to obtain the actual energy-saving potential across the units and improve the fluctuation resistance of the retrofitting schemes, a retrofitting method based on the actual cold and heat composite curves is put forward. Based on the industrial data of benzene production and C₈ units in a petrochemical enterprise, the heat exchanger networks of the two units are simulated in Aspen HYSYS and the pinch analysis is done with Aspen Energy Analyzer. Considering the unreasonable heat transfer of benzene production unit and the safety constraints, retrofitting schemes for the heat exchanger network of benzene production unit are proposed to reduce the steam consumption. Since the energy-saving potential of the C₈ unit is limited and the unreasonable heat transfer is distributed in different heat exchangers, it is not cost-effective to retrofit the heat exchanger network of the C₈ unit. The energy-saving potential of heat integration between the two units is analyzed by constructing the actual cold and hot composite curves. The advantage of using the actual cold and hot composite curves to guide the heat integration across the two units is that it uses the actual residual energy, which is more practical than the theoretical situation such as the grand composite curve. Besides, limitations and complexity of implementation are also considered to make retrofitting schemes. As a result, two heat integration retrofit schemes across the two units are proposed, compared, and discussed. The results show that the scheme with more energy saving needs more investment costs and has a slightly longer payback period, but has more economic benefits in the long term.
- actual composite curve /
- heat integration /
- pinch analysis /
- energy saving

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图 1 制苯装置总复合曲线

Figure 1. Grand compound curve of the benzene production unit

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图 2 制苯装置换热网络改造方案

Figure 2. Retrofit scheme of heat exchanger network for the benzene production unit

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图 3 碳八装置总复合曲线

Figure 3. Grand composite curve of the C₈ unit

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图 4 实际冷、热复合曲线

Figure 4. Actual cold and hot composite curves

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图 5 热联合方案1

Figure 5. Scheme 1 of heat integration across units

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图 6 热联合方案2

Figure 6. Scheme 2 of heat integration across units

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表 1 制苯装置换热器数据（B，H和C分别表示苯，热流和冷流）

Table 1. Data of heat exchangers in the benzene production unit (B, H, and C represent the benzene production unit, hot streams and cold streams, respectively)

Heat exchangers	Hot streams			Cold streams			Load /kW
Heat exchangers	Description	t_in/°C	t_out /°C	Description	t_in /°C	t_out /°C	Load /kW
E-102A/B	Medium pressure steam	—	—	BC1	124.7	127.0	4145
E-103	BH1	57.1	41.0	Cooling water	—	—	3127
E-1103	BH2	63.4	48.4	Cooling water	—	—	6053
E-1104A/B	Medium pressure steam	—	—	BC2	138.3	143.6	5462
E-1104N	BH3	180.0	165.0	BC2	138.3	143.6	1271
E-1111RN	BH4	138.3	75.0	BC3	30.0	45.79	309
E-202	BH5	84.4	40.0	Cooling water	—	—	40160
E-303N	BH6	131.1	98.1	BC4	80.0	99.6	823
E-304AN	BH7	285.6	125.6	BC4	99.6	243.6	7124
E-402	BH7	129.7	39.2	Cooling water	—	—	2553
E-408	BH6	155.0	131.1	BC5	103.3	128.1	641
EA-401	BH8	96.4	39.0	Cooling water	—	—	116
E-406	Medium pressure steam	—	—	BC6	155.1	158.0	819
EA-502	BH9	112.0	99.7	Air	—	—	5356
E-503	BH9	99.7	48.2	Cooling water	—	—	1326
E-109R	Medium pressure steam	—	—	BC6	155.7	158.7	3823
E-504	BH10	158.7	40.0	Cooling water	—	—	1063
E-3606	BH3	165.0	152.8	BC7	45.0	90.4	1010
E-3608	BH3	152.8	118.7	Cooling water	—	—	2733
E-3601	BH11	81.4	41.3	Cooling water	—	—	2800
E-3602A/B	High pressure steam	—	—	BC8	154.7	176.5	6370
E-3603	BH12	45.4	40.4	Cooling water	—	—	4694
E-3604	High pressure steam	—	—	BC9	204.2	205.0	2940
E-3605	BH3	208.0	180.0	BC10	144.3	167.7	2446
E-3609	BH3	160.1	55.0	Cooling water	—	—	189
E-3610	High pressure steam	—	—	BC9	157.3	160.1	129

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表 2 碳八装置的换热器数据（O，H，和C分别表示碳八，热流和冷流）

Table 2. Data of heat exchangers in the C₈ unit (O, H and C represent the C₈ unit, hot streams, and cold streams, respectively).

Heat exchangers	Hot streams			Cold streams			Load /kW
Heat exchangers	Description	t_in /°C	t_out /°C	Description	t_in /°C	t_out /°C	Load /kW
E-2111	OH1	120.5	40.0	Cooling water	—	—	309
E-2112	Low pressure steam	—	—	OC1	120.5	124.5	4583
E-2113	OH2	69.1	44.4	Cooling water	—	—	323
E-2201	OH3	33.0	29.0	Cooling water	—	—	38
E-2202	OH4	33.0	20.0	Cooling water	—	—	1
E-2301	OH5	100.0	95.0	OC2	40.0	73.5	99
E-2302	OH6	63.2	42.5	Cooling water	—	—	122
E-2304	OH6	42.5	6.2	Cooling water	—	—	2
E-2305	Low pressure steam	—	—	OC3	90.0	130.0	3437
E-2313	Low pressure steam	—	—	OC4	136.5	140.0	144
E-2308	OH5	95.0	79.8	Cooling water	—	—	293
E-2310	OH7	50.3	40.0	Cooling water	—	—	32
E-2312	Low pressure steam	—	—	OC5	101	120	1604
E-2307A	OH5	110.0	100.0	Cooling water	—	—	198
E-2400	OH8	69.5	12.7	Cooling water	—	—	1
E-2407	Ultra-low pressure steam	—	—	OC6	78.0	82.0	216
E-2411	OH9	81.5	52.0	Cooling water	—	—	48
E-2401	OH10	71.0	28.1	Cooling water	—	—	510
E-2403	OH11	32.0	30.7	Cooling water	—	—	2
E-2404	Ultra-low pressure steam	—	—	OC7	71.5	72.0	299
E-2405	OH11	67.0	32.0	Cooling water	—	—	40

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表 3 制苯装置现行换热网络的不合理换热

Table 3. Unreasonable heat transfer in the current heat exchanger network of benzene production unit

Heat exchangers		Load /kW	Unreasonable type
E-3608	1058		Cooler above the pinch point
E-3606	1010		Heat exchanger across the pinch point
E-304AN	433		Heat exchanger across the pinch point
E-408	325		Heat exchanger across the pinch point
E-504	187		Cooler above the pinch point
E-3609	143		Cooler above the pinch point
Total	3156

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表 4 制苯装置方案的投资成本和经济效益

Table 4. Investment costs and economic benefit of the scheme in the benzene production unit

Heat exchangers	Investment cost /10⁴ CNY	Economic benefits /10⁴ CNY/a
E-100	107.6	833.8
E-101	60.2	833.8

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表 5 碳八装置现行换热网络的不合理换热

Table 5. Unreasonable heat transfer in the current heat exchanger network of C₈ unit

Heat exchangers	Load/kW	Unreasonable type
E-2307A	198	Cooler above the pinch point
E-2308	159	Cooler above the pinch point
E-2111	135	Cooler above the pinch point
E-2301	94	Heat exchanger across the pinch point
Total	586

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表 6 热联合方案的投资成本和经济效益

Table 6. Investment costs and economic benefits of the schemes of heat integration across units

Schemes	Heat exchangers	Investment cost/10⁴ CNY	Economic benefits /10⁴ CNY/a
1	HCE-100	78.6	399.8
2	HCE-100	81.3	523.6
2	HCE-101	51.9	523.6

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