催化裂解气体脱硫装置技术改进

催化裂解气体脱硫装置第一周期开工中存在脱硫效果差、胺液再生效果不好以及胺耗过大等问题，采取更换脱硫剂、改进干气及酸性气脱液设施等技术改进措施，脱硫合格率由８８．５％提高到９８．３％，胺耗由０．８０ｋｇ／ｔ降到０．１２ｋｇ／ｔ胺液再生效果亦明显改善。     

天津炼油厂溶剂脱沥青装置

我厂溶剂脱沥青装置采用石化科学研究院提供的试验研究数据,并吸收引进美国UOP 公司胜利减压渣油 Demex 法专利技术,以大港减压渣油为原料,丁烷为溶剂,溶剂比6～7:1,加工能力为60万吨/年。一、技术特点1.抽提系统流程设计两个方案(1)塔内抽提流程:原料与溶剂逆向接触,重脱沥青油自塔顶至胶质沉降塔,分离出胶质溶液顶部脱沥青油进入高压溶剂回收部分。     

干气和液化气联合脱硫新工艺的探讨

为解决干气脱硫和液化气有机硫脱除率不高的问题，对同类装置进行了调研，结合中国石化前郭炼厂的实际情况，提出了在利用原有设备的基础上，新增部分设备就可达到干气和液化气联合脱硫目的的方案。     

炼厂气脱硫系统高效脱硫溶剂提浓降耗的模拟分析与工业验证

通过能量衡算分析了高效脱硫溶剂(XDS)的再生塔能耗构成。结果表明,加热胺液所需热量是再生塔再沸器热负荷的主要构成部分,对整个脱硫系统能耗影响最为显著。采用Aspen HYSYS流程模拟分析提高贫液中XDS含量对炼厂气脱硫系统再生塔能耗的影响,并在干气?液化气脱硫装置上进行了工业验证。模拟计算结果表明,提高贫液中XDS含量并降低其循环量可以在保证净化效果的前提下降低再生蒸汽耗量。工业试验结果与模拟值相吻合,贫液中XDS质量分数由23.82%提高到44.40%,再生塔的富液流量和相应的蒸汽耗量可分别降低20.4%和20.6%,节能降耗效果明显;XDS溶剂系统发泡倾向与腐蚀性均维持在较低水平,脱硫系统运行平稳。     

炼厂气脱硫系统高效脱硫溶剂提浓降耗的模拟分析与工业验证

通过能量衡算分析了高效脱硫溶剂（XDS）的再生塔能耗构成。结果表明,加热胺液所需热量是再生塔再沸器热负荷的主要构成部分,对整个脱硫系统能耗影响最为显著。采用Aspen HYSYS流程模拟分析提高贫液中XDS含量对炼厂气脱硫系统再生塔能耗的影响,并在干气/液化气脱硫装置上进行了工业验证。模拟计算结果表明,提高贫液中XDS含量并降低其循环量可以在保证净化效果的前提下降低再生蒸汽耗量。工业试验结果与模拟值相吻合,贫液中XDS质量分数由23.82%提高到44.40%,再生塔的富液流量和相应的蒸汽耗量可分别降低20.4%和20.6%,节能降耗效果明显;XDS溶剂系统发泡倾向与腐蚀性均维持在较低水平,脱硫系统运行平稳。     

脱硫装置水洗系统结垢原因分析及防治

针对液态烃脱硫装置水洗系统结垢状况,结合垢样分析数据,找出了发生结垢的诸多因素,并提出了用低温热水或蒸汽凝结水进行了水洗循环的有关措施。     

降低酮苯脱蜡装置溶剂排空损失的几项措施

文章主要论述了酮苯脱蜡装置溶剂排空损失与安全气的排空量和排空气体中的溶剂含量等两方面因素有关,并提出了从减少氮气补充量、减少漏入系统的空气量、选用合适的温洗溶剂温度、滤机温洗周期和温洗时间等方面入手以减少安全气排空量;从降低安全气中的溶剂含量和提高吸收塔效率等方面入手以降低排空气体中溶剂含量的一系列减少溶剂排空损失的解决措施。结果表明：通过应用这些解决措施可以明显降低酮苯脱蜡装置的溶剂排空损失,降低了溶剂消耗,节约了装置生产成本,也减少了环境污染。     

选择性脱硫溶剂在炼厂气脱硫装置上的应用

在炼厂气脱硫装置上，采用新型选择性甲基二乙醇胺脱硫溶剂取代了传统的单乙醇胺。实践结果证明，在不改造原有设备、流程的条件下，可获得稳定的合格的净化气体，同时给后续的克劳斯硫回收装置提供了富酸性气，并提出了优化选择性的操作条件。     

重催脱硫装置介绐

我厂重油催化裂化装置是一个１００万ｔ／ａ的特大型炼油装置,内设１１．８万ｔ／ａ液化气脱硫和脱硫酸装置,以及４．６万ｔ／ａ干气脱硫装置,采用二异丙醇胺脱硫。现将这两套脱硫装置的设计情况、试运转及标定验收情况以及随后的生产情况作一介绍。     

催化干气液化气脱硫技术改造

介绍某炼油厂催化裂化干气、液化气脱硫装置概况以及运行中存在的主要问题:胺液发泡、再生能力不足、液化气脱硫塔筛孔堵塞、液化气带胺等。装置于2004年进行扩能改造,采取更换液化气脱硫塔、更换胺液再生塔塔盘、增设胺液过滤器、更换新鲜胺液等措施,有效解决了装置运行中的瓶颈制约。提高了装置处理能力。改造后装置运行平稳,脱硫效果良好,产品质量合格。     

Desulfurization of FCC Gasoline by Solvent Extraction and Photooxidation

Abstract

A deep desulfurization process for FCC light gasoline has been investigated. The process is comprised of liquid-liquid extraction with acetonitrile, and photooxidation with ultraviolet light from a high-pressure mercury lamp. After the extraction the sulfur-containing compounds transfer from the oil to the solvent and then the solvent containing these sulfur compounds was photo-irradiated with ultraviolet light from a high pressure mercury lamp 300 W and with λ 200–300 nm, using strengthen electronic stirrer during the irradiation .The oil from the solvent was recovered with water. An azeotropic mixture (containing 86% acetonitrile and 14% water) was recovered successfully with one distillation column, and can reuse. The total sulfur content in this gasoline decreased from 309 to 68 ppm following 8 h of photo-irradiation .The total yield of the oil vary between 90–96%. The main sulfur compounds of this gasoline are alkyl substituted thiophenes.     

Desulfurization of FCC Gasoline by Solvent Extraction and Photooxidation

A deep desulfurization process for FCC light gasoline has been investigated. The process is comprised of liquid-liquid extraction with acetonitrile, and photooxidation with ultraviolet light from a high-pressure mercury lamp. After the extraction the sulfur-containing compounds transfer from the oil to the solvent and then the solvent containing these sulfur compounds was photo-irradiated with ultraviolet light from a high pressure mercury lamp 300 W and with λ 200-300 nm, using strengthen electronic stirrer during the irradiation .The oil from the solvent was recovered with water. An azeotropic mixture (containing 86% acetonitrile and 14% water) was recovered successfully with one distillation column, and can reuse. The total sulfur content in this gasoline decreased from 309 to 68 ppm following 8 h of photo-irradiation .The total yield of the oil vary between 90-96%. The main sulfur compounds of this gasoline are alkyl substituted thiophenes.     

Desulfurization of FCC Gas Oil by Solvent Extraction, Photooxidation, and Oxidizing Agents

A deep desulfurization process for FCC gas oil by a combination of liquid-liquid extraction, photochemical reaction, and treating with oxidation agents has been investigated. The process often represented by the model heterocyclic compounds, benzothiophenes (BTs) and dibenzothiophenes (DBTs). The process is comprised of three stages. Extraction of the sulfur-containing compounds from a catalytic cracked gas oil by acetonitrile, photooxidation, and photodecomposition of the sulphur compounds in the acetonitrile phase by ultraviolet irradiation from a high pressure mercury lamp, and recovery of the sulphur from the irradiated oil and treatment with oxidizing agent. The process was carried under conditions of room temperature and atmospheric pressure. Acetonitrile/water azeotropic mixture has been recycled successfully through distillation column. The sulfur in this gas oil has been decreased from 1800 ppm to 550 ppm after photo-desulfurization, and 508 ppm after treatment with the oxidizing agents. The total yield of the oil was 90-95%.     

天然气脱硫装置适应性模拟计算

天然气净化过程中,常常会遇到原料气气质条件发生变化的情况,此时需及时对过程的操作参数进行调整,以使过程高效平稳运行。本文利用流程模拟软件PROII,采用Amine物性包及Kent—Eisenberg模型,对某天然气净化厂天然气脱硫装置在原料气条件发生变化时的操作参数进行了适应性模拟计算。在验证计算模型的基础上,研究了原料气中H。S含量变化（6g／m3～16g／m3）、C02含量变化（25g／m3～45g／m3）、处理量变化（150×104m3／d～300×104m3／d）、温度变化（10℃～25℃）、压力变化（4．0MPa～6．0MPa）时,贫胺液循环量、贫胺液进料位置的调节范围。     

烟气湿法脱硫装置脱硫塔的腐蚀及防护

湿法烟气脱硫是国内除尘脱硫控制SO2排放的主要技术,其中EDV(非再生湿气洗涤工艺)和双循环湍冲文丘里技术应用最为广泛。脱硫装置接触介质复杂,介质腐蚀性强,造成脱硫塔塔壁腐蚀穿孔、烟囱腐蚀减薄、喷淋管及支撑梁断裂等,影响装置长周期运行。针对上述腐蚀等问题,分区域对金属塔和内衬非金属防腐涂料的塔体进行分析,从工艺控制、材料选用、结构优化、施工质量控制和操作运行等方面提出防腐蚀整改措施,效果良好。     

芳烃抽提装置的溶剂保护措施

中原石化总厂芳烃抽提装置通过采取一系列的保护措施,有效的减少了环丁砜溶剂的损耗,降低生产成本,综合经济效益明显提高。     

零售损耗的分环节控制与管理

就加油站数质量管理重点与难点的零售损耗问题,从油品的进、运、收、发四个环节阐述了对油品零售损耗的控制与管理,并介绍了各环节的重点工作及注意事项。     

麻石烟气脱硫装置耐酸胶泥的试验研究

文章对可用于麻石烟气脱硫装置的两种耐酸胶泥进行了单因素对比试验研究,结果表明,以水玻璃为粘合剂、氟硅酸钠为固化剂,燃煤电厂固体废料为填加剂的2号胶泥耐酸度较好,因而防腐蚀性能也较好,同时回收了燃煤电厂的固体废料,具有可观的环境效益。对水玻璃波美度、用量以及填料种类对胶泥性能的影响也进行了探讨。