半再生催化重整装置贫料和富料工艺流程的选择

以2套100 kt/a半再生催化重整装置为例,从预分馏、氢气流程以及重整产氢提纯方案工艺流程进行讨论分析,发现对贫料装置宜采用预加氢氢气循环和重整产氢再接触流程,对富料宜采用先分馏后加氢和重整产氢一次通过式流程.     

催化重整预处理两种工艺流程的分析比较

介绍了目前国内催化重整装置预处理部分先后馏后加氢加先加氢后分馏两种工艺流程。通过比较分析两种流程的优缺点，明确了呼和浩特石化公司催化重整装置预处理部分选择先加氢后分馏工艺的合理性。     

连续重整装置原料预处理单元优化效果分析

以中石化洛阳分公司70万t/a连续重整装置为例,介绍了对采取先分馏后加氢工艺流程的大冲量攻关优化。结果表明:增加石脑油进料换热器后,不仅预处理单元处理量有明显提高,而且拔头油中大于或等于C6组分的质量分数从38.77%降低到34.59%(其中拔头油中大于或等于C7组分的质量分数从9.29%降低到3.36%),重整进料中小于或等于C5组分的质量分数由1.73%减少到1.01%;同时优化了换热网络,彻底解决了石脑油预分馏塔进料温度不高带来的问题,实现了预处理单元大冲量优化攻关。     

柴油加氢改质装置的优化设计分析

针对2.3 Mt/a柴油加氢改质装置,对分馏系统及换热方案进行优化分析,分馏系统采用较优的汽提加分馏双塔流程,换热方案采用分馏塔底循环油与反应流出物进行换热,换热网络合理。并在多工况流程模拟的基础上对热高分温度、低分压力进行优化设计,从而降低了装置投资,减少了装置能耗。     

重整进料硫含量超标的原因及应对措施

分析了连续重整装置中硫含量超标的原因,认为是罐区精制石脑油中溶解的氧与重整原料预处理高分油中的H2S生成了不能靠蒸发汽提方式脱除的游离态硫导致的,通过实行停重整注硫泵、提高重整原料预处理反应温度等措施后,重整进料硫含量恢复正常。     

重整装置分馏系统氯腐蚀研究及工艺改进

陕西延长石油(集团)有限公司延安石油化工厂120万t/a连续重整装置设计之初未考虑脱除重整装置生成油中的氯,造成实际生产过程中后续分馏系统加氢生成氯化氢,遇水后发生严重腐蚀,影响装置长周期安全运行。通过对重整装置分馏系统设备腐蚀进行研究,对其现有工艺进行改进,增加重整油脱氯罐,从而解决了这一困扰装置长周期生产的问题。     

重整氢含氯对高换的腐蚀现状及防腐对策

在炼油行业加氢类装置中,重整氢是加氢类装置消耗氢气的主要来源之一,但是由于重整氢工艺流程的特点,与制氢装置产氢相比,其纯度较低、含氯较高。加氢装置使用重整氢气后,氢气中的氯与加氢反应生成的铵相结合,遇适宜温度后结晶,附着在设备表面,改变局部电化学环境,久而久之,便会造成设备的垢下腐蚀,对设备、产品质量和生产安全都有较大影响。     

1．2Mt／a重整装置进料硫含量超标原因与对策

对1．2Mt/a连续重整装置出现的重整进料硫含量超标的异常情况进行了分析,认为预加氢反应进料、出料换热器内漏、重整进料硫化剂注入过量、罐区来精制油中溶解氧与高分出料中的H2S反应生成不易汽提脱除的元素硫是硫含量超标的原因,通过采取检修换热器、暂停注硫泵、停止罐区来精制油进汽提塔等措施后,重整进料的硫含量达到了指标要求。     

80t/h酸性废水汽提装置工艺设计剖析

炼油厂常减压装置、尤里卡装置和延迟焦化装置等产生的大量含H2S酸性废水都采用汽提工艺回收H2S和氨。介绍了单塔汽提工艺和双塔汽提工艺各自的特点，阐述了单塔汽提工艺流程、主要设备的工艺参数和结构，指出单塔汽提工艺的能耗低，可获得合格的净化水。     

40万吨/年航煤加氢装置冷-2泄漏原因分析及对策

兰州石化公司炼油厂汽油加氢车间现有40万吨/年航煤加氢装置于1990年建成投产。最初设计为25万吨/年催化柴油加氢装置,根据生产需要,2000年4月装置扩建为40万吨/年航煤加氢装置,主要包括原料预处理系统、反应系统、分馏系统、辅助系统及公用工程,采用自动的单回路电动仪表控制。1现有工艺流程简述直馏煤油自67泵房或500万吨/年常减压装置来,经原料油过滤器（V23）过滤后进原料油缓冲罐（V11）、     

连续重整进料硫含量超高事故分析

简述了连续重整装置重整反应部分硫中毒的现象,通过分析得出罐区来的精制石脑油所带溶解氧与预加氢反应产生的硫化氢在汽提塔内生成单质硫,是引起硫含量偏高的原因。切断罐区来精制石脑油进汽提塔后,重整进料硫含量恢复正常。     

Alternate use of heavy hydrotreatment and visbreaker naphthas by incorporation into diesel

In order to provide a solution for refineries having limited catalytic reforming capacity, a process scheme for incorporating most of the low octane heavy hydrotreatment and visbreaker naphthas into diesel is presented in this paper. This scheme involves blending the visbreaker naphtha with the feed to the diesel hydrotreatment units, processing this blend at the usual conditions for diesel hydrodesulfurization and changing the cut point in the diesel stabilizer.     

Industrial application of an extended fully thermally coupled distillation column to BTX separation in a naphtha reforming plant

Aromatic compounds are yielded from naphtha reforming in a petrochemical plant, and the products are separated with binary distillation columns for benzene, toluene, xylene and heavy components in sequence. In this study, the first three columns of the fractionation process in the naphtha reforming unit are replaced with an extended fully thermally coupled distillation column (EFTCDC) also known as the extended Petlyuk column. An industrial-sized application of the EFTCDC is examined to compare the performance of the column with a conventional system. From a structural design giving the optimum structure of the column, a practical column structure is derived and used in the HYSYS simulation to find the optimal operation condition for a given set of product specifications. The EFTCDC gives an energy saving of 9.7% over a conventional three-column process. In addition, it is proved that the design procedure is good for an industrial process of 18 components.     

聚酯增容改造中工艺塔的模拟计算

建立工艺塔的数学模型 ,并且应用改进的三对角矩阵法对其进行了模拟计算。计算结果表明 ,对于水和乙二醇这种相对挥发度较大、易分离物系 ,精馏塔无需提馏段 ,而且精馏段理论塔板数仅为 4块 ,就能满足水和乙二醇的分离要求     

MOLECULAR MODELING AND OPTIMIZATION FOR CATALYTIC REFORMING

In this paper, molecular modeling and optimization for the naphtha catalytic reforming process is studied. The catalytic reforming process is for producing high octane number gasoline by reforming reactions in three sequencing fixed bed reactors. Feed naphtha coming from an atmospheric distillation unit consisted of molecules from C5 to C10 including paraffin, iso-paraffin, naphthene, and aromatic. The molecular reaction network consisted of paraffin cracking, naphthene side-chain cracking, aromatic side-chain cracking, ring opening, ring closure, paraffin isomerization, dehydrogenation, and hydrogenation. A molecular model for catalytic reforming was built. On the basis of the simulation model, a process optimization was performed for feed temperature and pressure under constraints such as benzene content, aromatic content, and RON (Research Octane Number) limitations. High RON was contrasted to low benzene and aromatic content requirements. By optimizing and controlling the reaction pathway, we can obtain a final product with the highest profit and appropriate benzene and aromatic contents and RON value. This example shows significant benefits from applying molecular modeling to optimization in the process level. Since gasoline production is related to many different processes such as reforming, FCC, isomerization, alkylation, and so on, more benefits can be obtained by applying molecular modeling to plant-wide optimization.     

MOLECULAR MODELING AND OPTIMIZATION FOR CATALYTIC REFORMING

In this paper, molecular modeling and optimization for the naphtha catalytic reforming process is studied. The catalytic reforming process is for producing high octane number gasoline by reforming reactions in three sequencing fixed bed reactors. Feed naphtha coming from an atmospheric distillation unit consisted of molecules from C5 to C10 including paraffin, iso-paraffin, naphthene, and aromatic. The molecular reaction network consisted of paraffin cracking, naphthene side-chain cracking, aromatic side-chain cracking, ring opening, ring closure, paraffin isomerization, dehydrogenation, and hydrogenation. A molecular model for catalytic reforming was built. On the basis of the simulation model, a process optimization was performed for feed temperature and pressure under constraints such as benzene content, aromatic content, and RON (Research Octane Number) limitations. High RON was contrasted to low benzene and aromatic content requirements. By optimizing and controlling the reaction pathway, we can obtain a final product with the highest profit and appropriate benzene and aromatic contents and RON value. This example shows significant benefits from applying molecular modeling to optimization in the process level. Since gasoline production is related to many different processes such as reforming, FCC, isomerization, alkylation, and so on, more benefits can be obtained by applying molecular modeling to plant-wide optimization.     

神府煤液化油石脑油馏分重整生产芳烃的研究

由于煤液化油石脑油馏分(200℃)中芳烃潜含量较高,利用煤液化油石脑油馏分为原料,进行加氢精制,将原料中的硫氮含量降至1 mg/kg左右,满足重整进料要求,然后在小型固定床连续反应器上进行加氢重整生产芳烃试验。着重考察重整反应前、后族组成的变化及主要芳烃化合物的产率。结果表明,加氢重整过程中发生正构烷烃异构化反应;环烷烃主要发生脱氢芳构化反应转化为芳香烃;煤液化油石脑油馏分适宜进行催化重整,C_1~C_4烃气产率6.03%,氢气产率3.60%;重整后,芳烃含量达83.20%,其中C_6~C_8芳烃含量61.03%,是提取BTX的良好原料。石脑油的馏程对芳烃的组成和产率有一定影响,适宜的馏程为60~160℃。     

分子筛预加氢及后加氢生产D40溶剂油和3#白油

利用分子筛脱蜡预加氢和后加氢装置改产D40溶剂油和3^#白油，现有原料条件下，生产出硫和氮含量均小于1 μg·g^-1的合格生成油，满足二段脱芳催化剂要求，各项主要指标达到设计值，特种溶剂油产品质量与国外同类油品质量相当。     

发展催化重整装置改善我国油品质量

针对我国汽油消耗量快速增长和油品指标日趋严格的现状,从芳烃及衍生物消费、加氢工艺氢源需求的增加等方面探讨了我国发展催化重整装置的重要性.指出制约我国催化重整发展的主要因素是与乙烯争夺原料,石脑油短缺问题.分析研究了扩大和优化催化重整原料来源的途径,以改变重整原料数量不足的局面.催化重整产品需求量的增加和原料供应的改善将使我国催化重整工艺进入一个新的发展时期.