制氢装置生产运行技术分析
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摘要
介绍了中国石油锦西石化公司5万m~3/h制氢装置负荷在52%、75%与101%时的生产运行状况。装置标定结果表明,低负荷运行时,通过提高水碳比和降低转化炉出口温度等优化措施,可保障转化炉平稳运行。分析了中变气换热系统出现空冷入口温度高的原因,提出了技术改造方案。介绍了PSA系统运行工况,产品氢纯度达到99.9%,低负荷时解吸气中氢气含量较高。装置101%负荷时能耗比设计值降低87.62个单位,52%与75%负荷时总能耗比设计值依次增加314.96、117.09个单位。
The 5×10~4 m~3/h hydrogen plant when running at 52%, 75% and 101% loads in Jinxi Petrochemical Company is analyzed in this paper. When the hydrogen plant is operating at low loads, the reformer operation is optimized through measures such as increasing the water-carbon ratio and reducing the outlet temperature of the reformer so as to ensure smooth operation of the reformer. The reasons of inlet temperature of the air cooler having exceeded design specifications are also analyzed, with technical retrofit presented. The operation conditions of the PSA system are introduced, and the hydrogen content in desorption gas should be higher when running at low loads to ensure the purity of hydrogen product up to 99.9%. The plant energy consumptions when working at 101%, 52% and 75% loads are 87.62 units lower, 314.96 units higher and 117.09 units higher respectively compared with design values.
The 5×10~4 m~3/h hydrogen plant when running at 52%, 75% and 101% loads in Jinxi Petrochemical Company is analyzed in this paper. When the hydrogen plant is operating at low loads, the reformer operation is optimized through measures such as increasing the water-carbon ratio and reducing the outlet temperature of the reformer so as to ensure smooth operation of the reformer. The reasons of inlet temperature of the air cooler having exceeded design specifications are also analyzed, with technical retrofit presented. The operation conditions of the PSA system are introduced, and the hydrogen content in desorption gas should be higher when running at low loads to ensure the purity of hydrogen product up to 99.9%. The plant energy consumptions when working at 101%, 52% and 75% loads are 87.62 units lower, 314.96 units higher and 117.09 units higher respectively compared with design values.
引文
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[11]马晓霞.制氢装置中温余热回收技术改造[J].炼油技术与工程,2009,39(5):55-57.
[12]崔欣,席林芳.制氢装置中温变换流程改造[J].炼油技术与工程,2014,44(3):9-11.
[2]朱赫礼,潘岩,陈金丹.国产催化剂在5万m3/h制氢装置的应用[J].炼油技术与工程,2015,45(7):47-50.
[3]陈金丹,朱赫礼,吴闯.国产催化剂在2×104 m3/h制氢装置的应用[J].齐鲁石油化工,2015,43(4):267-270.
[4]孙钦,何军成,郭竞标.焦化干气制氢技术的工业应用[J].石油炼制与化工,2003,34(9):6-10.
[5]王辉,常永胜.干气制氢装置低负荷运行时的操作优化[J].石化技术与应用,2012,30(2):156-159.
[6]周峰,辛华,段佳辉.制氢装置低负荷仅用富氢干气作原料工况的操作优化[J].炼油技术与工程,2013,43(11):22-24.
[7]柴保群,杨玉国.制氢装置中变气换热流程运行分析[J].炼油技术与工程,2014,44(5):34-38.
[8]马晓霞.制氢装置中温余热回收技术改造[J].炼油技术与工程,2009,39(5):55-57.
[9]崔欣,席林芳.制氢装置中温变换流程改造[J].炼油技术与工程,2014,44(3):9-11.
[10]柴保群,杨玉国.制氢装置中变气换热流程运行分析[J].炼油技术与工程,2014,44(5):34-38.
[11]马晓霞.制氢装置中温余热回收技术改造[J].炼油技术与工程,2009,39(5):55-57.
[12]崔欣,席林芳.制氢装置中温变换流程改造[J].炼油技术与工程,2014,44(3):9-11.