文献类型：期刊文献

英文题名：Corrigendum to "Techno-economic evaluation of post-combustion carbon capture based on chemical absorption for the thermal cracking furnace in ethylene manufacturing"(Fuel, (2023), 331, (125604), (S001623612202436X), 10.1016/j.fuel.2022.125604)

作者：Hu, Guihua[1]; Li, Xiaoxu[2]; Otitoju, Olajide[3]

机构：[1] Key Laboratory of Smart Manufacturing in Energy Chemical Process, Ministry of Education, School of Information Science and Engineering, East China University of Science and Technology, Shanghai, 200237, China; [2] Shanghai Smargo Logistics Services Co., Ltd, Shanghai, 200237, China; [3] Department of Chemical and Biological Engineering, The University of Sheffield, Sheffield, S1 3JD, United Kingdom

年份：2026

卷号：404

外文期刊名：Fuel

收录：EI(收录号：20255019690407)

语种：英文

摘要：The authors regret to report that there were errors in the published article. (1) The price of the blower was incorrectly recorded as M$5.74, which led to an error in the total equipment cost shown in Table 12. This discrepancy resulted in inaccurate capital expenditures (CAPEX) figures for the large-scale PCC plant in both Case 1 and Case 2, as presented in Table 14. Furthermore, this error affected the summary of the economic performance of the largescale PCC plant for both cases in Table 15. (2) The cost of low-pressure steam of PCC plant in Case 1 was reported as 1.139 M $/yr, which is incorrect. The original manuscript stated that the price of low-pressure steam was reduced to 0.0019 $/MJ, but the actual price should be 0.01085 $/MJ. In the original paper, the cost of low-pressure steam was incorrectly calculated as the sum of the low pressure steam cost of the reboiler (0.566 M $/yr) and the cross heat exchanger cost (0.573 M $/yr). In reality, it should only include the low-pressure steam cost of the reboiler (0.566 M $/yr). Therefore, the correct calculation of the low-pressure steam price for the device should be 3.23 M/yr. (3) The low-pressure steam cost of 0.548 M$/yr in Case 2 in Table 15 is incorrect. This cost calculation is based on a low price of lowpressure steam of 0.0019 $/MJ and includes the cost of the lowpressure steam used in the reboiler. However, as mentioned previously in (2) above, the actual price of low-pressure steam has increased, making the calculated cost lower than the actual cost. To address this issue, we will divide Case 2 into two separate cases. The first case will account for the cost of low-pressure steam in the reboiler, while the second case will assume that the low-pressure steam in the reboiler is supplied at no cost due to excess heat from the gasoline fractionator. Based on the current price of low-pressure steam at 0.01085 $/MJ, the calculated costs for these two cases are $3.14 million per year and $0, respectively. (4) Table 13 selects propane as the refrigerant. However, the price of 42347.2 $/tonne is too high. According to the freezing requirements in this article, air refrigerant (2712.50 $/tonne) would be a cheaper alternative. The specific corrections made are outlined below Abstract, lines 11–13 The results indicate that the cost of CO2 capture can be reduced from $85.24/tonne without heat integration to $81.74/tonne when lowpressure steam costs are taken into account. Additionally, with heat integration and without considering low-pressure steam costs, the cost can be reduced to $41.49/tonne. When considering the impact of carbon credits on capture costs, the cost can be further reduced from $65.24/ tonne to $61.74/tonne by including low-pressure steam cost. Without considering low-pressure steam costs, the price can drop to $21.49/. ? 2025 Elsevier Ltd.