技术领域technical field
本实用新型涉及一种有机氧化物催化转化制芳烃的系统。The utility model relates to a system for producing aromatic hydrocarbons through catalytic conversion of organic oxides.
背景技术Background technique
芳烃是一种重要的有机化工基础原料，其中苯、甲苯和二甲苯(包括邻二甲苯、间二甲苯和对二甲苯)用途十分广泛，其终端产品用于合成树脂、合成纤维、合成橡胶、涂料、染料和医药等领域。随着我国经济社会发展，对芳烃的需求也日益增长，目前我国每年芳烃的消耗量超过2000万吨，但是有一半需从国外进口。Aromatics is an important organic chemical basic raw material, among which benzene, toluene and xylene (including o-xylene, m-xylene and p-xylene) are widely used, and their end products are used in synthetic resin, synthetic fiber, synthetic rubber, Coatings, dyes and pharmaceuticals and other fields. With the development of my country's economy and society, the demand for aromatics is also increasing. At present, the annual consumption of aromatics in my country exceeds 20 million tons, but half of them need to be imported from abroad.
苯、甲苯和二甲苯主要来源于石油化工工业，国内石油化工路线生产的芳烃约占芳烃生产总量85％以上，生产技术主要包括：石脑油催化重整、乙烯裂解石脑油加氢抽提和低碳烃类芳构化等，其中石脑油催化重整芳烃产量约占石油化工路线芳烃产量的80％，乙烯裂解石脑油加氢抽提芳烃产量约占16％。随着石油资源的日益枯竭，原油价格居高不下，给石油化工路线制取芳烃带来了较大的成本压力。我国的能源现状是多煤少油缺气，20世纪90年代以来伴随经济的持续增长，我国对外石油依赖度不断增加，1993年至1996年，我国对外石油依赖度基本在10％以内，到2000年首次超过30％，2007年达到50.5％，2013年达到57.39％，远超过国际上公认的30％警戒线。然后，我国煤炭资源丰富，近年来在国家政策支持下，煤制甲醇、二甲醚和乙二醇等行业迅速发展，据统计2013年我国甲醇产量近2900万吨。因此，发展有机氧化物催化转化制芳烃技术以替代传统的石油化工路线，可以降低芳烃对石油原料的依赖度，对我国能源安全和芳烃生产行业有着重要的作用。Benzene, toluene and xylene mainly come from the petrochemical industry. The aromatics produced by domestic petrochemical routes account for more than 85% of the total aromatics production. The production technologies mainly include: naphtha catalytic reforming, ethylene cracking naphtha hydrogenation pumping Extraction and aromatization of low-carbon hydrocarbons, etc. Among them, the output of aromatics from catalytic reforming of naphtha accounts for about 80% of the output of aromatics in petrochemical routes, and the output of aromatics from ethylene cracking naphtha hydroextraction accounts for about 16%. With the increasing depletion of petroleum resources, the price of crude oil remains high, which has brought greater cost pressure to the production of aromatics in petrochemical routes. my country's current energy situation is more coal, less oil and less gas. Since the 1990s, with the continuous economic growth, my country's dependence on foreign oil has continued to increase. From 1993 to 1996, my country's dependence on foreign oil was basically within 10%. By 2000 It exceeded 30% for the first time in 2007, reached 50.5% in 2007, and reached 57.39% in 2013, far exceeding the internationally recognized warning line of 30%. Then, my country is rich in coal resources. In recent years, under the support of national policies, industries such as coal-to-methanol, dimethyl ether and ethylene glycol have developed rapidly. According to statistics, my country's methanol production in 2013 was nearly 29 million tons. Therefore, the development of catalytic conversion of organic oxides to aromatics to replace the traditional petrochemical route can reduce the dependence of aromatics on petroleum raw materials, which plays an important role in my country's energy security and aromatics production industry.
利用有机氧化物催化转化制芳烃的技术，最早由美国美孚石油公司提出，其1979年申请的专利US4156698 A公开了利用含有分子筛的复合催化剂将C1-C4醇类或醚类化合物转化为低碳烯烃和芳烃的方法；1985年申请的专利US4590321A中公开了利用ZSM-5或ZSM-11等分子筛催化剂将C2-C12烷烃、C2-C12烯烃、C1-C5醇类和C2-C12醚类等非芳烃化合物转化为芳烃的工艺；美国专利US4686312 A、US4724270 A、US4822939 A、US4822939 A和US4049573 A等也公开了在不同催化剂作用下甲醇或二甲醚制芳烃的方法。但这些美国专利的重点主要在于研究催化剂组成以及反应操作条件对芳烃转化率和选择性的影响，个别专利提出甲醇或二甲醚制芳烃的反应流程，但均没有明确提出有机氧化物制芳烃技术的反应再生系统、反应再生方法以及反应器和再生器型式。The technology of using organic oxides to convert aromatics was first proposed by Mobil Oil Company of the United States. The patent US4156698 A applied for in 1979 disclosed the use of composite catalysts containing molecular sieves to convertC1 -C4 alcohols or ethers into low The method of carbon olefins and aromatics; the patent US4590321A that applied for in 1985 discloses utilizing molecular sieve catalysts such as ZSM-5 or ZSM-11 to C2 -C12 alkanes, C2 -C12 olefins, C1 -C5 alcohols and The process of converting non-aromatic compounds such as C2 -C12 ethers into aromatics; U.S. Patents US4686312 A, US4724270 A, US4822939 A, US4822939 A and US4049573 A, etc. also disclose the process of producing aromatics from methanol or dimethyl ether under the action of different catalysts method. However, the focus of these U.S. patents is mainly to study the influence of catalyst composition and reaction operating conditions on the conversion rate and selectivity of aromatics. Some patents propose the reaction process of methanol or dimethyl ether to aromatics, but none of them clearly proposes the technology of organic oxides to aromatics The reaction regeneration system, reaction regeneration method and reactor and regenerator type.
目前，国内也有多家研究院所对有机氧化物制芳烃技术进行研发，主要包括清华大学、中国科学院山西煤炭化学研究所、中国石化上海石油化工研究院和中国科学院大连化学物理研究所等。中国专利CN 1880288A公开了以甲醇为原料在改性ZSM-5分子筛催化剂作用下制芳烃的工艺，该专利将一段反应器甲醇芳构化气相产物冷却后分离出低碳烃类和液相产物，液相产物经萃取分离得到芳烃和非芳烃，低碳烃类进入二段反应器进一步芳构化，从而提高芳烃的总选择性。中国专利CN 101823929 B提出了一种甲醇或二甲醚制取芳烃的系统和工艺，甲醇或二甲醚先在芳构化反应器反应，反应产物中氢气、甲烷、混合C8芳烃和部分C9+烃类作为产品，C2+非芳烃和除混合C8芳烃及部分C9+烃类之外的芳烃则会循环到另一个反应器进行进一步芳构化，提高芳烃的收率和选择性。中国专利CN 101607858 B、CN 102190546B、CN 102371176 B和CN 102371177 B等也分别公开了有机氧化物催化转化制芳烃工艺和有机氧化物催化转化制芳烃催化剂及制备方法。上述专利同样着重于考察不同催化剂组成以及稀有金属、稀土金属改性对芳构化过程的影响，CN 1880288A和CN 101823929 B主要提出反应产物循环芳构化对芳烃收率的影响，但这些专利仍未涉及有机氧化物制芳烃的反应再生系统。At present, there are also a number of research institutes in China conducting research and development on the technology of producing aromatics from organic oxides, mainly including Tsinghua University, Shanxi Institute of Coal Chemistry, Chinese Academy of Sciences, Sinopec Shanghai Petrochemical Research Institute, and Dalian Institute of Chemical Physics, Chinese Academy of Sciences. Chinese patent CN 1880288A discloses a process for producing aromatics using methanol as a raw material under the action of a modified ZSM-5 molecular sieve catalyst. In this patent, the gas phase product of methanol aromatization in the first stage reactor is cooled to separate low-carbon hydrocarbons and liquid phase products. The liquid phase product is extracted and separated to obtain aromatics and non-aromatics, and the low-carbon hydrocarbons enter the second-stage reactor for further aromatization, thereby improving the overall selectivity of aromatics. Chinese patent CN 101823929 B proposes a system and process for preparing aromatics from methanol or dimethyl ether. Methanol or dimethyl ether is first reacted in an aromatization reactor, and the reaction products include hydrogen, methane, mixedC8 aromatics and some C9+ hydrocarbons as products, C2+ non-aromatics and aromatics except mixed C8 aromatics and some C9+ hydrocarbons will be recycled to another reactor for further aromatization, improving the yield and selection of aromatics sex. Chinese patents CN 101607858 B, CN 102190546B, CN 102371176 B, and CN 102371177 B also disclose the process of producing aromatics by catalytic conversion of organic oxides and catalysts for producing aromatics by catalytic conversion of organic oxides and their preparation methods. The above-mentioned patents also focus on investigating the influence of different catalyst compositions and the modification of rare metals and rare earth metals on the aromatization process. CN 1880288A and CN 101823929 B mainly propose the influence of cyclic aromatization of reaction products on the yield of aromatic hydrocarbons, but these patents still It does not involve the reaction regeneration system of organic oxides to aromatics.
中国专利CN 101244969 A公开了一种连续芳构化与催化剂再生的装置及其方法，该装置包括一个芳构化流化床与一个催化剂连续再生的流化床及设置在两个流化床之间的用于催化剂输送的管道和固体输送装置，但该专利并未提出再生系统的具体形式，并且存在一些问题：再生器只设一级气固分离系统，催化剂回收率低，造成昂贵的催化剂跑损严重；再生器型式为单段床层再生，为保证催化剂再生效率，再生温度最高可达750℃，由于催化剂夹带的焦炭中含有部分氢，燃烧后生成水，在高温和水蒸汽作用下催化剂水热失活严重，导致催化剂活性降低；再生器取热方式为内取热，并且只设置一根取热盘管，当盘管爆裂时取热介质大量窜入再生器，会导致再生器压力迅速升高，严重时甚至会引起爆炸。Chinese patent CN 101244969 A discloses a device and method for continuous aromatization and catalyst regeneration. The pipelines and solid conveying devices used for catalyst transportation, but the patent does not propose the specific form of the regeneration system, and there are some problems: the regenerator is only equipped with a gas-solid separation system, and the catalyst recovery rate is low, resulting in expensive catalysts. Severe running loss; the regenerator type is single-stage bed regeneration. In order to ensure the catalyst regeneration efficiency, the regeneration temperature can reach up to 750°C. Since the coke entrained by the catalyst contains some hydrogen, water will be generated after combustion. Under the action of high temperature and water vapor The hydrothermal deactivation of the catalyst is serious, which leads to the reduction of the catalyst activity; the regenerator takes internal heat, and only one heat-taking coil is installed. When the coil bursts, a large amount of heat-taking medium enters the regenerator, which will cause the regenerator The pressure rises rapidly, and in severe cases, it may even cause an explosion.
实用新型内容Utility model content
本实用新型的目的是提供一种有机氧化物催化转化制芳烃的系统，该系统既能满足提高芳烃产品收率和选择性的要求，又适合于有机氧化物催化转化制芳烃工业化连续生产，同时可以大幅度降低催化剂跑损和水热失活，降低工业化有机氧化物催化转化制芳烃的成本。The purpose of this utility model is to provide a system for producing aromatics by catalytic conversion of organic oxides, which can meet the requirements of improving the yield and selectivity of aromatics products, and is suitable for the industrial continuous production of aromatics by catalytic conversion of organic oxides. It can greatly reduce catalyst running loss and hydrothermal deactivation, and reduce the cost of producing aromatics by catalytic conversion of industrial organic oxides.
为了实现上述目的，本实用新型提供一种有机氧化物催化转化制芳烃的系统，该系统包括反应器1和再生器2；其特征在于，所述反应器1包括上下连通的反应器稀相段4和密相床层反应段3，且所述反应器稀相段4位于所述密相床层反应段3的上方；所述密相床层反应段3的底部设置有用于分布送入所述密相床层反应段3的所述有机氧化物的进料分布板10，所述进料分布板10位于所述密相床层反应段3下部的再生剂入口的下方；所述再生器2包括第一再生器5和第二再生器6；所述密相床层反应段3上部的待生剂出口与所述第一再生器5上部的待生剂入口连通，所述第一再生器5下部的半再生剂出口与所述第二再生器6下部的半再生剂入口连通，所述第二再生器6的再生剂出口与所述密相床层反应段3下部的所述再生剂入口连通。In order to achieve the above purpose, the utility model provides a system for catalytic conversion of organic oxides to aromatics, the system includes a reactor 1 and a regenerator 2; it is characterized in that the reactor 1 includes a dilute phase section of the reactor connected up and down 4 and the dense phase bed reaction section 3, and the dilute phase section 4 of the reactor is located above the dense phase bed reaction section 3; the bottom of the dense phase bed reaction section 3 is provided with a The feed distribution plate 10 of the organic oxide in the dense phase bed reaction section 3, the feed distribution plate 10 is located below the regenerant inlet at the bottom of the dense phase bed reaction section 3; the regenerator 2 includes a first regenerator 5 and a second regenerator 6; the spent agent outlet on the upper part of the dense-phase bed reaction section 3 communicates with the spent agent inlet on the upper part of the first regenerator 5, and the first regenerator The outlet of the semi-regenerated agent at the lower part of the device 5 communicates with the inlet of the semi-regenerated agent at the lower part of the second regenerator 6, and the outlet of the regenerated agent at the lower part of the second regenerator 6 communicates with the regenerated agent at the lower part of the dense-phase bed reaction section 3. The agent inlet is connected.
优选地，其特征在于，所述反应器稀相段4内设置有至少一组相互串连的反应器一级旋风分离器11和反应器二级旋风分离器12。Preferably, it is characterized in that at least one set of reactor primary cyclone separators 11 and reactor secondary cyclone separators 12 are arranged in the dilute phase section 4 of the reactor.
优选地，其特征在于，所述密相床层反应段3上部的所述待生剂出口通过待生剂上斜管14与用于汽提待生剂所夹带油气的待生剂汽提器7连通；所述待生剂汽提器7通过待生剂下斜管16与所述第一再生器5上部的所述待生剂入口连通，或依次通过待生剂下斜管16和待生剂提升管18与所述第一再生器5上部的所述待生剂入口连通；所述待生剂下斜管16上设置有用于控制所述反应器1催化剂料位的待生滑阀17；所述待生剂汽提器7腔体内的底部设置有用于均匀分布送入所述待生剂汽提器7的汽提介质的汽提介质分布管15。Preferably, it is characterized in that the outlet of the spent agent on the upper part of the dense-phase bed reaction section 3 passes through the inclined pipe 14 of the spent agent and the spent agent stripper for stripping the entrained oil and gas of the spent agent. 7 communicated; the spent agent stripper 7 is communicated with the spent agent inlet on the top of the first regenerator 5 through the spent agent drop pipe 16, or sequentially through the spent spent agent down inclined pipe 16 and the spent agent The raw agent riser 18 is in communication with the said raw agent inlet on the upper part of the first regenerator 5; the said raw agent descending pipe 16 is provided with a waiting slide valve for controlling the catalyst level of the reactor 1 17: The bottom of the cavity of the spent agent stripper 7 is provided with a stripping medium distribution pipe 15 for evenly distributing the stripping medium sent into the spent agent stripper 7 .
优选地，其特征在于，所述第一再生器5腔体内的底部设置有用于均匀分布送入所述第一再生器5的再生含氧气体的含氧气体分布环20，第二再生器6腔体内的底部设置有用于均匀分布送入所述第二再生器6的再生含氧气体的含氧气体分布管19。Preferably, it is characterized in that the bottom of the cavity of the first regenerator 5 is provided with an oxygen-containing gas distribution ring 20 for evenly distributing the regenerated oxygen-containing gas sent into the first regenerator 5, and the second regenerator 6 An oxygen-containing gas distribution pipe 19 for evenly distributing the regenerated oxygen-containing gas sent to the second regenerator 6 is arranged at the bottom of the cavity.
优选地，其特征在于，所述第一再生器5的上部设置为稀相床区段，下部设置为密相床区段；所述第一再生器5上部的所述待生剂入口位于所述第一再生器5的所述稀相床区段的下部；所述第一再生器5的所述稀相床区段内设置有至少一组相互串连的第一再生器一级旋风分离器21和第一再生器二级旋风分离器22。Preferably, it is characterized in that the upper part of the first regenerator 5 is set as a dilute-phase bed section, and the lower part is set as a dense-phase bed section; the spent agent inlet on the upper part of the first regenerator 5 is located at the The lower part of the dilute-phase bed section of the first regenerator 5; the dilute-phase bed section of the first regenerator 5 is provided with at least one group of first regenerator primary cyclone separation in series 21 and the first regenerator secondary cyclone separator 22.
优选地，其特征在于，所述第一再生器5与所述第二再生器6为上下重叠设置，且所述第二再生器6顶部的烟气出口与所述第一再生器5的底部通过低压降分布板连通。Preferably, it is characterized in that the first regenerator 5 and the second regenerator 6 are stacked up and down, and the flue gas outlet at the top of the second regenerator 6 is connected to the bottom of the first regenerator 5 Communication through the low pressure drop distribution plate.
优选地，其特征在于，所述第一再生器5的所述半再生剂出口通过半再生上斜管28与用于脱除半再生催化剂所夹带烟气的半再生脱气管9连通；所述半再生脱气管9通过半再生下斜管30与所述第二再生器6的所述半再生剂入口连通；所述半再生下斜管30上设置有用于控制所述第一再生器5催化剂料位的半再生滑阀31；所述半再生脱气管9腔体内的底部设置有用于均匀分布送入所述半再生脱气管9的半再生剂脱气介质的半再生剂脱气介质分布环29。Preferably, it is characterized in that the semi-regenerated agent outlet of the first regenerator 5 communicates with the semi-regenerated degassing pipe 9 for removing the entrained flue gas of the semi-regenerated catalyst through a semi-regenerated upper inclined pipe 28; The semi-regenerated degassing pipe 9 communicates with the semi-regenerated agent inlet of the second regenerator 6 through a semi-regenerated downslope 30; The semi-regenerated slide valve 31 of the material level; the bottom in the cavity of the semi-regenerated degassing pipe 9 is provided with a semi-regenerated agent degassing medium distribution ring for evenly distributing the semi-regenerated agent degassing medium sent into the semi-regenerated degassing pipe 9 29.
优选地，其特征在于，所述第一再生器5与所述第二再生器6为并列设置，所述第二再生器6的上部设置为稀相床区段，下部设置为密相床区段；所述第二再生器6下部的所述半再生剂入口位于所述第二再生器6的密相床区段的底部，所述第二再生器6的所述再生剂出口位于所述第二再生器6的密相床区段的上部；所述第二再生器6的稀相床区段内设置有至少一组相互串连的第二再生器一级旋风分离器34和第二再生器二级旋风分离器35。Preferably, it is characterized in that the first regenerator 5 and the second regenerator 6 are arranged in parallel, the upper part of the second regenerator 6 is set as a dilute-phase bed section, and the lower part is set as a dense-phase bed section section; the semi-regenerated agent inlet of the lower part of the second regenerator 6 is located at the bottom of the dense bed section of the second regenerator 6, and the regenerated agent outlet of the second regenerator 6 is located at the The upper part of the dense-phase bed section of the second regenerator 6; the dilute-phase bed section of the second regenerator 6 is provided with at least one group of second regenerator primary cyclone separator 34 and the second regenerator in series. Regenerator secondary cyclone separator 35.
优选地，其特征在于，所述第一再生器5底部的所述半再生剂出口依次通过半再生下斜管30和半再生剂提升管33与所述第二再生器6密相床区段的底部的所述半再生剂入口连通，或直接通过半再生下斜管30与所述第二再生器6密相床区段的底部的所述半再生剂入口连通；所述半再生下斜管30上设置有用于控制所述第一再生器5催化剂料位的半再生滑阀31。Preferably, it is characterized in that the outlet of the semi-regenerated agent at the bottom of the first regenerator 5 passes through the semi-regenerated downcomer 30 and the semi-regenerated agent riser 33 in sequence with the dense bed section of the second regenerator 6 The semi-regenerated agent inlet at the bottom of the bottom is communicated, or directly communicates with the semi-regenerated agent inlet at the bottom of the second regenerator 6 dense bed section through the semi-regenerated downslope pipe 30; the semi-regenerated downslope The pipe 30 is provided with a semi-regeneration slide valve 31 for controlling the catalyst level of the first regenerator 5 .
优选地，其特征在于，所述第二再生器6的所述再生剂出口通过再生剂上斜管24与用于脱除再生催化剂所夹带烟气的再生剂脱气罐8连通；所述再生剂脱气罐8依次通过再生剂下斜管26和再生剂提升管32与所述密相床层反应段3下部的所述再生剂入口连通，或直接通过再生剂下斜管26与所述密相床层反应段3下部的再生剂入口连通；所述再生剂下斜管26上设置有用于控制所述第二再生器6催化剂料位的再生滑阀27；所述再生剂脱气罐8腔体内的底部设置有用于均匀分布送入所述再生剂脱气罐8的再生剂脱气介质的再生剂脱气介质分布环25。Preferably, it is characterized in that the outlet of the regenerant of the second regenerator 6 communicates with the regenerant degassing tank 8 for removing the entrained flue gas of the regenerated catalyst through a regenerant upward inclined pipe 24; The agent degassing tank 8 communicates with the regenerant inlet at the lower part of the dense-phase bed reaction section 3 through the regenerant downslope 26 and the regenerant riser 32 successively, or directly connects with the regenerant through the regenerant downslope 26. The regenerant inlet at the lower part of the dense-phase bed reaction section 3 is communicated; the regenerant descending pipe 26 is provided with a regeneration slide valve 27 for controlling the catalyst level of the second regenerator 6; the regenerant degassing tank 8 The bottom of the cavity is provided with a regenerant degassing medium distribution ring 25 for evenly distributing the regenerated agent degassing medium sent into the regenerated agent degassing tank 8 .
本实用新型提供的有机氧化物催化转化制芳烃的系统具有如下优点：The system for preparing aromatics by catalytic conversion of organic oxides provided by the utility model has the following advantages:
1、有机氧化物催化转化制芳烃反应和催化剂再生分别在反应器和再生器内进行，两器之间斜管均设置脱气设施，反应原料及产品与烧焦用含氧气体基本不接触，过程安全平稳，可实现连续操作；1. The catalytic conversion of organic oxides to aromatics and catalyst regeneration are carried out in the reactor and the regenerator respectively. The inclined pipes between the two devices are equipped with degassing facilities, and the reaction raw materials and products are basically not in contact with the oxygen-containing gas used for charring. The process is safe and stable, and continuous operation can be realized;
2、设置了两个再生器，第一再生器可以设置为低温贫氧操作，第二再生器可以设置为高温富氧操作，在最大程度上降低催化剂水热失活的同时，可以降低烧焦用含氧气体用量，从而降低有机氧化物催化转化制芳烃的操作成本；2. Two regenerators are set up. The first regenerator can be set for low-temperature oxygen-poor operation, and the second regenerator can be set for high-temperature oxygen-enriched operation, which can reduce the scorch while reducing the hydrothermal deactivation of the catalyst to the greatest extent. Use the amount of oxygen-containing gas to reduce the operating cost of catalytic conversion of organic oxides to aromatics;
3、反应器和再生器均设置至少一组两级旋风分离器，尽可能回收反应产物和烟气中夹带的催化剂，可以降低催化剂损耗和操作成本，还可以减少反应产物后续冷却分离系统的管线和设备磨损、以及烟气排放带来的环境污染。3. Both the reactor and the regenerator are equipped with at least one set of two-stage cyclone separators to recover the catalyst entrained in the reaction product and flue gas as much as possible, which can reduce catalyst loss and operating costs, and can also reduce the pipeline of the subsequent cooling and separation system of the reaction product and equipment wear, as well as environmental pollution caused by flue gas emissions.
本实用新型的其他特征和优点将在随后的具体实施方式部分予以详细说明。Other features and advantages of the present utility model will be described in detail in the following specific embodiments.
附图说明Description of drawings
附图是用来提供对本实用新型的进一步理解，并且构成说明书的一部分，与下面的具体实施方式一起用于解释本实用新型，但并不构成对本实用新型的限制。在附图中：The accompanying drawings are used to provide a further understanding of the utility model, and constitute a part of the description, together with the following specific embodiments, are used to explain the utility model, but do not constitute a limitation to the utility model. In the attached picture:
图1是本实用新型的有机氧化物催化转化制芳烃系统的第一种具体实施方式(即重叠式两段再生，待生催化剂输送线路采用提升风提升)；Fig. 1 is the first specific embodiment of the system for producing aromatics by catalytic conversion of organic oxides of the present invention (i.e. overlapping two-stage regeneration, the transmission line of the catalyst to be born is lifted by lifting wind);
图2是本实用新型的有机氧化物催化转化制芳烃系统的第二种具体实施方式(即重叠式两段再生，再生催化剂输送线路采用提升风提升)；Fig. 2 is the second specific embodiment of the system for producing aromatics by catalytic conversion of organic oxides of the present invention (i.e. overlapping two-stage regeneration, the regenerated catalyst transmission line adopts lifting wind to lift);
图3是本实用新型的有机氧化物催化转化制芳烃系统的第三种具体实施方式(即重叠式两段再生，待生催化剂和再生催化剂输送线路均采用提升风提升)；Fig. 3 is the third specific embodiment of the system for producing aromatics by catalytic conversion of organic oxides of the present invention (i.e. overlapping two-stage regeneration, both the waiting catalyst and the regenerated catalyst transmission lines are lifted by lifting wind);
图4是本实用新型的有机氧化物催化转化制芳烃系统的第四种具体实施方式(即并列式两段再生，半再生催化剂输送线路采用提升风提升)。Fig. 4 is the fourth specific embodiment of the system for producing aromatics by catalytic conversion of organic oxides of the present invention (that is, parallel two-stage regeneration, semi-regenerated catalyst transmission line adopts lifting wind to lift).
附图标记说明Explanation of reference signs
1反应器 2再生器 3密相床层反应段 4反应器稀相段5第一再生器 6第二再生器 7待生剂汽提器 8再生剂脱气罐9半再生脱气管 10进料分布板 11反应器一级旋风分离器12反应器二级旋风分离器 13反应器集气室 14待生剂上斜管15汽提介质分布管 16待生剂下斜管 17待生滑阀18待生剂提升管 19含氧气体分布管 20含氧气体分布环21第一再生器一级旋风分离器 22第一再生器二级旋风分离器23第一再生器集气室 24再生剂上斜管 25再生剂脱气介质分布环26再生剂下斜管 27再生滑阀 28半再生上斜管29半再生剂脱气介质分布环 30半再生下斜管 31半再生滑阀32再生剂提升管 33半再生剂提升管 34第二再生器一级旋风分离器35第二再生器二级旋风分离器 36第二再生器集气室1 Reactor 2 Regenerator 3 Dense phase bed reaction section 4 Dilute phase section of reactor 5 First regenerator 6 Second regenerator 7 Regenerated agent stripper 8 Regenerated agent degassing tank 9 Semi-regenerated degassing pipe 10 Feed Distribution plate 11 Primary cyclone separator of reactor 12 Secondary cyclone separator of reactor 13 Gathering chamber of reactor 14 Inclined pipe for raw agent 15 Distribution pipe for stripping medium 16 Lower inclined pipe for raw agent 17 Slide valve for raw agent 18 Regenerated agent riser 19 Oxygen-containing gas distribution pipe 20 Oxygen-containing gas distribution ring 21 Primary cyclone separator of the first regenerator 22 Secondary cyclone separator of the first regenerator 23 Gathering chamber of the first regenerator 24 Regenerative agent upward slope Pipe 25 Regenerant degassing medium distribution ring 26 Regenerated agent lower inclined pipe 27 Regenerated slide valve 28 Semi-regenerated upper inclined pipe 29 Semi-regenerated agent degassed medium distribution ring 30 Semi-regenerated lower inclined pipe 31 Semi-regenerated slide valve 32 Regenerated agent riser 33 Semi-regenerator riser 34 Second regenerator primary cyclone separator 35 Second regenerator secondary cyclone separator 36 Second regenerator gas collection chamber
具体实施方式Detailed ways
以下结合附图对本实用新型的具体实施方式进行详细说明。应当理解的是，此处所描述的具体实施方式仅用于说明和解释本实用新型，并不用于限制本实用新型。The specific embodiment of the utility model will be described in detail below in conjunction with the accompanying drawings. It should be understood that the specific embodiments described here are only used to illustrate and explain the utility model, and are not intended to limit the utility model.
本实用新型提供一种有机氧化物催化转化制芳烃的系统，该系统包括反应器1和再生器2；其特征在于，所述反应器1包括上下连通的反应器稀相段4和密相床层反应段3，且所述反应器稀相段4位于所述密相床层反应段3的上方；所述密相床层反应段3的底部设置有用于分布送入所述密相床层反应段3的所述有机氧化物的进料分布板10，所述进料分布板10位于所述密相床层反应段3下部的再生剂入口的下方；所述再生器2包括第一再生器5和第二再生器6；所述密相床层反应段3上部的待生剂出口与所述第一再生器5上部的待生剂入口连通，所述第一再生器5下部的半再生剂出口与所述第二再生器6下部的半再生剂入口连通，所述第二再生器6的再生剂出口与所述密相床层反应段3下部的所述再生剂入口连通。The utility model provides a system for producing aromatics by catalytic conversion of organic oxides, the system includes a reactor 1 and a regenerator 2; it is characterized in that the reactor 1 includes a reactor dilute phase section 4 and a dense phase bed connected up and down layer reaction section 3, and the dilute phase section 4 of the reactor is located above the dense phase bed reaction section 3; the bottom of the dense phase bed reaction section 3 is provided with a The feed distribution plate 10 of the organic oxide in the reaction section 3, the feed distribution plate 10 is located below the regenerant inlet of the lower part of the dense-phase bed reaction section 3; the regenerator 2 includes a first regeneration device 5 and the second regenerator 6; the spent agent outlet at the upper part of the dense-phase bed reaction section 3 communicates with the spent agent inlet at the upper part of the first regenerator 5, and the half of the lower part of the first regenerator 5 The regenerant outlet communicates with the semi-regenerant inlet at the lower part of the second regenerator 6 , and the regenerant outlet of the second regenerator 6 communicates with the regenerant inlet at the lower part of the dense bed reaction section 3 .
根据本实用新型，所述有机氧化物和用于有机氧化物催化转化制芳烃的催化剂均为本领域技术人员所熟知，例如，所述有机氧化物可以为选自C1-C10醇类、C2-C12醚类和C3-C12酮类中的至少一种；所述催化剂可以为含有分子筛和载体的微球催化剂，所述分子筛优选为ZSM-5分子筛。According to the present utility model, the organic oxide and the catalyst used for the catalytic conversion of the organic oxide to aromatics are well known to those skilled in the art. For example, the organic oxide can be selected from C1 -C10 alcohols, At least one of C2 -C12 ethers and C3 -C12 ketones; the catalyst may be a microsphere catalyst containing a molecular sieve and a carrier, and the molecular sieve is preferably a ZSM-5 molecular sieve.
根据本实用新型，所述密相床层反应段3为密相床区段，反应器稀相段4为稀相床区段，设置密相床区段是为了控制有机氧化物在反应床层的停留时间，保证原料甲醇与催化剂间的充分高效接触，抑制大气泡和催化剂团聚物生成，从而维持较高的反应转化率和芳烃选择性；设置稀相床区段是为了使反应产品气在较低流速下靠重力初步分离夹带的催化剂，并且有足够的空间布置两级旋风分离器进一步分离催化剂，减少催化剂跑损和催化剂对后续设备和管道的磨损，为了增加反应器内的催化剂藏量及方便旋风分离器的翼阀设置在密相床层中以减少催化剂跑损，反应器1中实际处于密相流化态的催化剂层的高度可以没过旋风分离器的翼阀，这是本领域技术人员所熟知的。采用本实用新型进行芳构化反应时，优选的反应条件如下：密相床层反应段3的反应温度为400-600℃，反应器稀相段4的反应压力为0.05-0.6MPa(g)，密相床层反应段质量空速为0.1-10小时-1，有机氧化物在密相床层反应段的停留时间为5-30秒。然而，本领域技术人员也可以根据实际反应的需要来设置芳构化反应的条件，本实用新型并没有限制。According to the utility model, the dense-phase bed reaction section 3 is a dense-phase bed section, and the dilute-phase section 4 of the reactor is a dilute-phase bed section. The dense-phase bed section is set to control the organic oxide in the reaction bed The residence time of the catalyst is guaranteed to ensure sufficient and efficient contact between the raw material methanol and the catalyst, and the formation of large bubbles and catalyst agglomerates is suppressed, thereby maintaining a high reaction conversion rate and aromatics selectivity; the purpose of setting the dilute bed section is to make the reaction product gas flow in the The entrained catalyst is preliminarily separated by gravity at a lower flow rate, and there is enough space to arrange a two-stage cyclone separator to further separate the catalyst, reducing catalyst loss and catalyst wear on subsequent equipment and pipelines, in order to increase the catalyst storage in the reactor And the wing valve of the convenient cyclone separator is set in the dense phase bed to reduce the loss of catalyst, the height of the catalyst layer actually in the dense phase fluidized state in the reactor 1 can not exceed the wing valve of the cyclone separator, which is this well known to those skilled in the art. When adopting the utility model to carry out the aromatization reaction, the preferred reaction conditions are as follows: the reaction temperature of the dense phase bed reaction section 3 is 400-600°C, and the reaction pressure of the dilute phase section 4 of the reactor is 0.05-0.6MPa (g) , the mass space velocity of the dense bed reaction section is 0.1-10 hours-1 , and the residence time of the organic oxide in the dense bed reaction section is 5-30 seconds. However, those skilled in the art can also set the conditions of the aromatization reaction according to the needs of the actual reaction, which is not limited by the present invention.
根据本实用新型，所述反应系统可以设置有至少一组两级旋风分离器进行所述反应产物与待生催化剂的分离，例如，所述反应器稀相段4内可以设置有至少一组相互串连的反应器一级旋风分离器11和反应器二级旋风分离器12。所述旋风分离器是本领域技术人员所熟知的，本实用新型不再赘述。一般一组两级旋风分离器包括串联的一个一级旋风分离器和一个二级旋风分离器；当设置多组两级旋风分离器时，一级旋风分离器和二级旋风分离器的数量一般相同，之间可以通过一级升气管一对一连接，也可以将多个一级旋风分离器的升气管汇合成一个集合管后，再与多个二级旋风分离器连接，二级旋风分离器的二级升气管均与集气室连接，所述集气室可以设在反应器稀相段4的内部，也可以设在反应器稀相段4的外部。需要说明的是，本实用新型再生器内所述的旋风分离器也均可如此设置，下文将不再赘述。According to the utility model, the reaction system can be provided with at least one set of two-stage cyclone separators to separate the reaction product from the unborn catalyst, for example, at least one set of mutual A reactor primary cyclone separator 11 and a reactor secondary cyclone separator 12 are connected in series. Said cyclone separator is well known to those skilled in the art, and will not be repeated in this utility model. Generally, a set of two-stage cyclone separators includes a first-stage cyclone separator and a second-stage cyclone separator connected in series; Similarly, they can be connected one-to-one through the first-stage air riser, or the air risers of multiple first-stage cyclone separators can be merged into a collection pipe, and then connected to multiple second-stage cyclone separators, and the second-stage cyclone separation The secondary gas risers of the reactor are all connected to the gas collection chamber, and the gas collection chamber can be arranged inside or outside the dilute phase section 4 of the reactor. It should be noted that the cyclone separator described in the regenerator of the present invention can also be set in this way, which will not be described in detail below.
根据本实用新型，可以将反应后的待生催化剂从所述密相床层反应段3上部的待生剂上斜管14引出反应器1，经汽提后输送至第一再生器5。根据本实用新型的一种具体实施方式，所述密相床层反应段3上部的所述待生剂出口可以通过待生剂上斜管14与用于汽提待生剂所夹带油气的待生剂汽提器7连通；所述待生剂汽提器7腔体内的底部可以设置有用于均匀分布送入所述待生剂汽提器7的汽提介质的汽提介质分布管15。其中，所述待生剂汽提器7的作用是汽提反应后待生剂所夹带的部分反应产物，以减少产品损失。所述待生剂汽提器7内可以设置有1个或多个汽提介质分布管15用来分布汽提介质，所述汽提介质可以包括但不限于选自蒸汽、氮气、甲烷、干气和燃料气中的至少一种。According to the utility model, the reacted spent catalyst can be drawn out of the reactor 1 from the inclined tube 14 on the upper part of the dense-phase bed reaction section 3, and transported to the first regenerator 5 after being stripped. According to a specific embodiment of the present invention, the outlet of the spent agent on the upper part of the dense-phase bed reaction section 3 can pass through the inclined pipe 14 of the spent agent and the standby agent for stripping the oil and gas entrained in the spent agent. The raw agent stripper 7 communicates; the bottom in the cavity of the spent agent stripper 7 can be provided with a stripping medium distribution pipe 15 for evenly distributing the stripping medium sent into the spent agent stripper 7 . Wherein, the role of the spent agent stripper 7 is to strip part of the reaction product entrained by the spent agent after the reaction, so as to reduce product loss. One or more stripping medium distribution pipes 15 may be provided in the spent agent stripper 7 to distribute the stripping medium, and the stripping medium may include but not limited to be selected from steam, nitrogen, methane, dry At least one of gas and fuel gas.
根据密相床层反应段3的待生剂出口与第一再生器1的待生剂入口的高度不同，待生剂由密相床层反应段3向第一再生器5的输送方式有两种：当密相床层反应段3的待生剂出口比第一再生器5的待生剂入口高较多时，待生剂可以通过自重自流至第一再生器5中；当密相床层反应段3的待生剂出口比第一再生器5待生剂入口低、相同或高出不多时，待生剂可以通过提升风送入第一再生器5中，即所述待生剂汽提器7可以通过待生剂下斜管16与所述第一再生器5上部的所述待生剂入口连通(如图2、4所示)，或可以依次通过待生剂下斜管16和待生剂提升管18与所述第一再生器5上部的所述待生剂入口连通(如图1、3所示)；所述待生剂下斜管16上可以设置有用于控制所述反应器1催化剂料位的待生滑阀17。所述待生剂提升管18内可以送入提升风，所述提升风可以包括但不限于选自含氧气体、氮气和蒸汽中的至少一种。According to the difference in height between the outlet of the spent agent in the dense-phase bed reaction section 3 and the inlet of the spent agent in the first regenerator 1, there are two ways for the spent agent to be transported from the dense-phase bed reaction section 3 to the first regenerator 5. Kind: when the outlet of the spent agent in the dense-phase bed reaction section 3 is higher than the inlet of the spent agent in the first regenerator 5, the spent agent can flow into the first regenerator 5 by its own weight; when the dense-phase bed When the outlet of the spent agent in the reaction section 3 is lower, the same or slightly higher than the inlet of the spent agent in the first regenerator 5, the spent agent can be sent into the first regenerator 5 by the lifting wind, that is, the spent agent vapor The lifter 7 can be communicated with the spent agent inlet on the top of the first regenerator 5 through the spent agent drop pipe 16 (as shown in Figures 2 and 4), or can pass through the spent agent drop pipe 16 And the spent agent riser 18 is communicated with the described spent agent inlet on the first regenerator 5 top (as shown in Figure 1, 3); Described spent agent descending inclined pipe 16 can be provided with for controlling all The standby slide valve 17 for the catalyst material level of the reactor 1. Lifting wind can be fed into the spent agent riser 18, and the lifting wind can include but not limited to at least one selected from oxygen-containing gas, nitrogen and steam.
本实用新型的发明人发现，有机氧化物催化转化制芳烃催化剂在高温和高水蒸汽分压时水热失活较为明显，因此本实用新型上下重叠布置或并列布置两个再生器对待生催化剂进行两段再生，以降低催化剂的高温水热失活。即所述第一再生器5可以为采用第一含氧气体的贫氧操作，再生温度可以为500-650℃，并且由于焦炭中氢的燃烧速度远远大于碳的燃烧速度，待生催化剂在第一再生器较为缓和的再生条件下，可烧掉焦炭中50重％-90重％的碳元素和60重％-100重％的氢元素，以体积计，第一再生器5所产生烟气中一氧化碳和二氧化碳的比例可以为0.2-3。虽然大部分氢元素可以在第一再生器5中烧掉变成水蒸汽，但由于烧焦温度较低，可以有效减小催化剂的水热失活。第二再生器6可以为采用第二含氧气体的富氧操作，再生温度可以为600-750℃，再生条件比第一再生器6苛刻，由于焦炭中氢元素在第一再生器5内基本燃烧完全，第二再生器6可以在高温低水蒸汽分压的条件下将催化剂上10重％-50重％的碳元素和0重％-40重％的氢元素完全燃烧，以减少催化剂的水热失活。以体积计，第二再生器6所产生烟气中氧气的含量可以为0.5-15体％。当所述待生催化剂进行第二再生后，以重量计并以催化剂的总重量为基准，再生催化剂中焦炭的含量可以为0.01-0.1重％。当然，本领域技术人员也可以根据实际情况在本实用新型的再生系统中采用其它再生方法对有机氧化物催化转化制芳烃催化剂进行再生，本实用新型没有限制。The inventors of the present utility model have found that the hydrothermal deactivation of catalysts for producing aromatics by catalytic conversion of organic oxides is relatively obvious at high temperature and high water vapor partial pressure, so the present utility model arranges two regenerators overlapping up and down or arranged side by side to treat the raw catalyst Two-stage regeneration to reduce high-temperature hydrothermal deactivation of the catalyst. That is to say, the first regenerator 5 can be an oxygen-lean operation using the first oxygen-containing gas, and the regeneration temperature can be 500-650° C., and since the combustion rate of hydrogen in coke is much higher than that of carbon, the catalyst to be regenerated is Under relatively gentle regeneration conditions of the first regenerator, 50% to 90% by weight of carbon and 60% to 100% by weight of hydrogen in the coke can be burned. The ratio of carbon monoxide and carbon dioxide in the air can be 0.2-3. Although most of the hydrogen can be burnt into water vapor in the first regenerator 5, the hydrothermal deactivation of the catalyst can be effectively reduced due to the low burning temperature. The second regenerator 6 can be an oxygen-enriched operation using a second oxygen-containing gas, the regeneration temperature can be 600-750°C, and the regeneration conditions are harsher than the first regenerator 6, because the hydrogen element in the coke is basically in the first regenerator 5 Combustion is complete, the second regenerator 6 can completely burn the carbon element of 10 weight %-50 weight % and the hydrogen element of 0 weight %-40 weight % on the catalyst under the condition of high temperature and low water vapor partial pressure, to reduce the Hydrothermal inactivation. On a volume basis, the oxygen content in the flue gas generated by the second regenerator 6 may be 0.5-15% by volume. After the second regeneration of the spent catalyst, the content of coke in the regenerated catalyst may be 0.01-0.1% by weight based on the total weight of the catalyst. Of course, those skilled in the art can also use other regeneration methods in the regeneration system of the present invention to regenerate the catalyst for catalytic conversion of organic oxides to aromatics according to the actual situation, and the present invention is not limited.
根据本实用新型，为保证再生含氧气体在第一再生器5和第二再生器6内分布均匀且与催化剂充分接触，以达到良好的烧焦效果和流化状态，所述第一再生器5腔体内的底部可以设置有用于均匀分布送入所述第一再生器5的再生含氧气体的含氧气体分布环20，第二再生器6腔体内的底部可以设置有用于均匀分布送入所述第二再生器6的再生含氧气体的含氧气体分布管19。其中，所述含氧气体分布环20上应该至少设置1根耐磨短管；所述含氧气体分布管19一般采用树枝状分布管，每个树枝状的分支管上也应该至少设置1根耐磨短管，因此含氧气体分布管19对气体的分布效果一般要优于含氧气体分布环。According to the utility model, in order to ensure that the regenerated oxygen-containing gas is evenly distributed in the first regenerator 5 and the second regenerator 6 and fully contacts with the catalyst, so as to achieve a good charring effect and a fluidized state, the first regenerator 5, the bottom of the chamber can be provided with an oxygen-containing gas distribution ring 20 for evenly distributing the regenerated oxygen-containing gas sent into the first regenerator 5, and the bottom of the second regenerator 6 chamber can be provided with a ring 20 for evenly distributing the regenerated oxygen-containing gas The oxygen-containing gas distribution pipe 19 for regenerating the oxygen-containing gas of the second regenerator 6 . Wherein, the oxygen-containing gas distribution ring 20 should be provided with at least one wear-resistant short pipe; the oxygen-containing gas distribution pipe 19 generally adopts a dendritic distribution pipe, and each dendritic branch pipe should also be provided with at least one Wear-resistant short pipe, so the gas distribution effect of the oxygen-containing gas distribution pipe 19 is generally better than that of the oxygen-containing gas distribution ring.
根据本实用新型，所述第一再生器5的上部可以设置为稀相床区段，下部可以设置为密相床区段，为了增加再生器内的催化剂藏量及方便旋风分离器的翼阀设置在密相床层中以减少催化剂跑损，第一再生器中实际处于密相流化态的催化剂层的高度可以高于第一再生器的待生剂入口的高度，也可以没过旋风分离器的翼阀；所述第一再生器5上部的所述待生剂入口可以位于所述第一再生器5的所述稀相床区段的下部；所述第一再生器5的所述稀相床区段内可以设置有至少一组相互串连的第一再生器一级旋风分离器21和第一再生器二级旋风分离器22。According to the utility model, the upper part of the first regenerator 5 can be set as a dilute-phase bed section, and the lower part can be set as a dense-phase bed section. Set in a dense-phase bed to reduce catalyst loss, the height of the catalyst layer actually in a dense-phase fluidized state in the first regenerator can be higher than the height of the spent agent inlet of the first regenerator, or it can be submerged in the cyclone The flap valve of the separator; the spent agent inlet at the upper part of the first regenerator 5 may be located at the lower part of the dilute bed section of the first regenerator 5; At least one set of the first regenerator primary cyclone separator 21 and the first regenerator secondary cyclone separator 22 connected in series may be arranged in the dilute bed section.
根据本实用新型，所述第一再生器5与所述第二再生器6可以为上下重叠设置，且所述第二再生器6顶部的烟气出口可以与所述第一再生器5的底部通过低压降分布板连通，如图1-3所示。所述低压降分布板可以允许气体通过，但仅允许少量催化剂通过。所述第一再生器5的所述半再生剂出口可以通过半再生上斜管28与用于脱除半再生催化剂所夹带烟气的半再生脱气管9连通；所述半再生脱气管9可以通过半再生下斜管30与所述第二再生器6的所述半再生剂入口连通；所述半再生下斜管30上可以设置有用于控制所述第一再生器5催化剂料位的半再生滑阀31，可以通过控制所述半再生脱气管9的催化剂流出量来控制所述第一再生器5的催化剂料位；所述半再生脱气管9腔体内的底部可以设置有用于均匀分布送入所述半再生脱气管9的半再生剂脱气介质的半再生剂脱气介质分布环29。所述半再生脱气管9为本领域技术人员所熟知，其作用是减少半再生催化剂夹带的烟气，增大半再生下斜管30内催化剂密度以提高半再生滑阀31的压差，保证半再生滑阀31的平稳操作。半再生脱气管9可以设置至少1个半再生剂脱气介质分布环29，脱气介质可以包括但不限于选自蒸汽、氮气、空气和其它惰性气体中的至少一种。According to the present utility model, the first regenerator 5 and the second regenerator 6 can be overlapped up and down, and the flue gas outlet at the top of the second regenerator 6 can be connected to the bottom of the first regenerator 5 Connected through the low pressure drop distribution plate, as shown in Figure 1-3. The low pressure drop distribution plate allows gas to pass through, but only a small amount of catalyst. The semi-regenerated agent outlet of the first regenerator 5 can communicate with the semi-regenerated degassing pipe 9 for removing the entrained flue gas of the semi-regenerated catalyst through the semi-regenerated upper inclined pipe 28; the semi-regenerated degassing pipe 9 can be The semi-regenerated agent inlet of the second regenerator 6 is communicated with the semi-regenerated downcomer 30; The regeneration slide valve 31 can control the catalyst level of the first regenerator 5 by controlling the catalyst outflow of the semi-regenerated degassing pipe 9; the bottom in the cavity of the semi-regenerated degassing pipe 9 can be provided with The semi-regenerated agent degassing medium distribution ring 29 of the semi-regenerated agent degassing medium sent into the semi-regenerated degassing pipe 9 . The semi-regenerated degassing pipe 9 is well known to those skilled in the art, and its function is to reduce the flue gas entrained by the semi-regenerated catalyst, increase the catalyst density in the semi-regenerated descending pipe 30 to increase the pressure difference of the semi-regenerated slide valve 31, and ensure the semi-regenerated Smooth operation of regeneration spool valve 31. The semi-regenerated degassing pipe 9 can be provided with at least one semi-regenerated agent degassing medium distribution ring 29, and the degassing medium can include but not limited to at least one selected from steam, nitrogen, air and other inert gases.
根据本实用新型，所述第一再生器5与所述第二再生器6可以为并列设置，如图4所示，所述第二再生器6的上部可以设置为稀相床区段，下部可以设置为密相床区段，为了增加再生器内的催化剂藏量及方便旋风分离器的翼阀设置在密相床层中以减少催化剂跑损，第二再生器中实际处于密相流化态的催化剂层的高度可以没过旋风分离器的翼阀；所述第二再生器6下部的所述半再生剂入口可以位于所述第二再生器6的密相床区段的底部，所述第二再生器6的所述再生剂出口可以位于所述第二再生器6的密相床区段的上部；所述第二再生器6的稀相床区段内可以设置有至少一组相互串连的第二再生器一级旋风分离器34和第二再生器二级旋风分离器35。According to the utility model, the first regenerator 5 and the second regenerator 6 can be arranged side by side, as shown in FIG. 4 , the upper part of the second regenerator 6 can be set as a dilute-phase bed section, and the lower part It can be set as a dense-phase bed section. In order to increase the catalyst storage in the regenerator and facilitate the cyclone separator’s wing valve to be set in the dense-phase bed to reduce catalyst loss, the second regenerator is actually in dense-phase fluidization The height of the catalyst layer in the state can not cross the wing valve of the cyclone separator; the inlet of the semi-regenerated agent in the lower part of the second regenerator 6 can be located at the bottom of the dense bed section of the second regenerator 6, so The regenerant outlet of the second regenerator 6 may be located on the upper part of the dense-phase bed section of the second regenerator 6; at least one set of The first-stage cyclone separator 34 of the second regenerator and the second-stage cyclone separator 35 of the second regenerator are connected in series.
在本实用新型中，根据并列设置的两个再生器相对标高不同，半再生催化剂由第一再生器向第二再生器的输送方式可以有两种：当第一再生器5的底部比第二再生器6的底部高较多时，所述第一再生器5底部的所述半再生剂出口可以直接通过半再生下斜管30与所述第二再生器6密相床区段的底部的所述半再生剂入口连通，半再生催化剂可以直接由半再生下斜管30通过自重自流至第二再生器6的底部；当第一再生器5的底部比第二再生器6的底部要低或者相同甚至略高一点时，所述第一再生器5底部的所述半再生剂出口可以依次通过半再生下斜管30和半再生剂提升管33与所述第二再生器6密相床区段的底部的所述半再生剂入口连通，半再生催化剂可以由半再生下斜管30流至半再生剂提升管33，再利用半再生剂提升管33中的提升风输送半再生催化剂至第二再生器6的底部。另外，所述半再生下斜管30上可以设置有用于控制所述第一再生器5催化剂料位的半再生滑阀31。需要说明的是，本实用新型中，“下部”包括“底部”，即“第一再生器5下部”包括“第一再生器5底部”。In the present utility model, according to the difference in relative elevation of the two regenerators arranged side by side, there are two ways to transport the semi-regenerated catalyst from the first regenerator to the second regenerator: when the bottom of the first regenerator 5 is lower than the second When the bottom of the regenerator 6 is relatively high, the outlet of the semi-regenerated agent at the bottom of the first regenerator 5 can directly pass through the semi-regenerated downcomer 30 and the bottom of the dense-phase bed section of the second regenerator 6. The semi-regenerated agent inlet is connected, and the semi-regenerated catalyst can directly flow to the bottom of the second regenerator 6 from the semi-regenerated downcomer 30 by its own weight; when the bottom of the first regenerator 5 is lower than the bottom of the second regenerator 6 or When the same or even slightly higher, the outlet of the semi-regenerated agent at the bottom of the first regenerator 5 can pass through the semi-regenerated downcomer 30 and the semi-regenerated agent riser 33 and the dense bed area of the second regenerator 6 in sequence. The semi-regenerated agent inlet at the bottom of the section is connected, and the semi-regenerated catalyst can flow from the semi-regenerated descending pipe 30 to the semi-regenerated agent riser 33, and then utilize the lifting wind in the semi-regenerated agent riser 33 to transport the semi-regenerated catalyst to the second The bottom of the second regenerator 6 . In addition, the semi-regeneration downcomer 30 may be provided with a semi-regeneration slide valve 31 for controlling the catalyst material level of the first regenerator 5 . It should be noted that in the present invention, "lower part" includes "bottom", that is, "lower part of the first regenerator 5" includes "bottom of the first regenerator 5".
根据本实用新型，所述第二再生器6的所述再生剂出口可以通过再生剂上斜管24与用于脱除再生催化剂所夹带烟气的再生剂脱气罐8连通。根据第二再生器与反应器的相对标高不同，所述再生剂脱气罐8可以依次通过再生剂下斜管26和再生剂提升管32与所述密相床层反应段3下部的所述再生剂入口连通(如图2、3所示)，或可以直接通过再生剂下斜管26与所述密相床层反应段3下部的再生剂入口连通(如图1、4所示)；所述再生剂下斜管26上可以设置有用于控制所述第二再生器6催化剂料位的再生滑阀27；所述再生剂脱气罐8腔体内的底部可以设置有用于均匀分布送入所述再生剂脱气罐8的再生剂脱气介质的再生剂脱气介质分布环25。为保证脱气效果，减少进入反应器中的非烃组分以降低反应产物压缩机能耗，再生剂脱气罐8可以设置有至少1个再生剂脱气介质分布环25；所述脱气介质可以包括但不限于选自蒸汽、氮气和其它惰性气体中的至少一种。According to the present invention, the regenerant outlet of the second regenerator 6 can communicate with the regenerant degassing tank 8 for removing the entrained flue gas of the regenerated catalyst through the regenerant upward inclined pipe 24 . According to the relative elevation difference between the second regenerator and the reactor, the regenerant degassing tank 8 can be connected to the lower part of the dense-phase bed reaction section 3 through the regenerant downslope 26 and the regenerant riser 32 in sequence. The regenerant inlet is communicated (as shown in Figures 2 and 3), or can be directly communicated with the regenerant inlet of the dense-phase bed reaction section 3 bottom through the regenerant downslope 26 (as shown in Figures 1 and 4); The regeneration slide valve 27 for controlling the catalyst material level of the second regenerator 6 may be provided on the descending pipe 26 of the regenerant; the bottom of the cavity of the regenerant degassing tank 8 may be provided with a The regenerant degassing medium distribution ring 25 of the regenerated agent degassing medium of the regenerated agent degassing tank 8 . In order to ensure the degassing effect and reduce the non-hydrocarbon components entering the reactor to reduce the energy consumption of the reaction product compressor, the regenerant degassing tank 8 can be provided with at least one regenerant degassing medium distribution ring 25; the degassing medium It may include but not limited to at least one selected from steam, nitrogen and other inert gases.
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520058029.5UCN204474555U (en) | 2015-01-28 | 2015-01-28 | A kind of system of organic oxygen compound catalytic cracking aromatic hydrocarbons |
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520058029.5UCN204474555U (en) | 2015-01-28 | 2015-01-28 | A kind of system of organic oxygen compound catalytic cracking aromatic hydrocarbons |
| Publication Number | Publication Date |
|---|---|
| CN204474555Utrue CN204474555U (en) | 2015-07-15 |
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520058029.5UExpired - LifetimeCN204474555U (en) | 2015-01-28 | 2015-01-28 | A kind of system of organic oxygen compound catalytic cracking aromatic hydrocarbons |
| Country | Link |
|---|---|
| CN (1) | CN204474555U (en) |
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107540495A (en)* | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | Methanol or the method for dimethyl ether conversion production aromatic hydrocarbons and low-carbon alkene |
| CN107540498A (en)* | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | By methanol or the method for dimethyl ether conversion preparing aromatic hydrocarbon and low-carbon alkene |
| CN107540492A (en)* | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | By methanol or the method for dimethyl ether production aromatic hydrocarbons and low-carbon alkene |
| CN107540496A (en)* | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | Methanol or the method for dimethyl ether production aromatic hydrocarbons and low-carbon alkene |
| CN108017484A (en)* | 2016-11-04 | 2018-05-11 | 中国石油化工股份有限公司 | The method of high arenes selectivity during maintenance methanol aromatic hydrocarbons |
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107540495A (en)* | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | Methanol or the method for dimethyl ether conversion production aromatic hydrocarbons and low-carbon alkene |
| CN107540498A (en)* | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | By methanol or the method for dimethyl ether conversion preparing aromatic hydrocarbon and low-carbon alkene |
| CN107540492A (en)* | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | By methanol or the method for dimethyl ether production aromatic hydrocarbons and low-carbon alkene |
| CN107540496A (en)* | 2016-06-29 | 2018-01-05 | 中国石油化工股份有限公司 | Methanol or the method for dimethyl ether production aromatic hydrocarbons and low-carbon alkene |
| CN108017484A (en)* | 2016-11-04 | 2018-05-11 | 中国石油化工股份有限公司 | The method of high arenes selectivity during maintenance methanol aromatic hydrocarbons |
| CN108017484B (en)* | 2016-11-04 | 2020-09-04 | 中国石油化工股份有限公司 | Method for maintaining high aromatic selectivity in process of preparing aromatic hydrocarbon from methanol |
| Publication | Publication Date | Title |
|---|---|---|
| CN204474555U (en) | A kind of system of organic oxygen compound catalytic cracking aromatic hydrocarbons | |
| CN110818521B (en) | Device and method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compound | |
| CN101850276B (en) | Catalyst regeneration method for improving selectivity of catalyst | |
| CN103073377B (en) | A kind of oxygenatedchemicals catalyzed conversion prepares the method for low-carbon alkene | |
| CN105985209B (en) | A kind of method of organic oxide catalytic cracking aromatic hydrocarbons | |
| US10844289B2 (en) | Chemical looping processes for catalytic hydrocarbon cracking | |
| CN110818522B (en) | Device and method for preparing aromatic hydrocarbon and low-carbon olefin from oxygen-containing compound | |
| CN103446959B (en) | A kind of fluidized-bed reactor with charging heat exchange, reaction regeneration device and application thereof | |
| CN103664444A (en) | Method of producing ethylene and propylene by using waste catalytic cracking catalyst | |
| CN111807916B (en) | Device for producing low-carbon olefin by efficient oxygen-containing compound | |
| CN101850274A (en) | A Catalyst Regeneration Method for Improving Catalyst Selectivity | |
| CN103055961B (en) | Catalyst regeneration method with characteristic of emission reduction | |
| CN105461497B (en) | The two-stage regeneration reaction unit and its reaction method of methanol and/or dimethyl ether conversion producing light olefins and aromatic hydrocarbons | |
| CN204469680U (en) | The regenerative system of a kind of organic oxygen compound catalytic cracking arenes catalytic agent | |
| CN103071434A (en) | Internal circulation gas-solid fluidized bed reactor | |
| CN105983454B (en) | A kind of regeneration method of organic oxide catalytic cracking arenes catalytic agent | |
| CN204469711U (en) | The regenerative system of a kind of organic oxygen compound catalytic cracking arenes catalytic agent | |
| CN108017486B (en) | Method for preparing aromatic hydrocarbon by converting oxygen-containing compound-containing raw material | |
| CN105983455B (en) | A kind of regeneration method of organic oxide catalytic cracking arenes catalytic agent | |
| CN104117328B (en) | The catalytic conversion system of successive reaction-regeneration and method | |
| CN113366089B (en) | Process for converting naphtha-containing feedstock to lower olefins and aromatics | |
| CN103102937A (en) | Catalytic cracking method for reducing carbon dioxide emission | |
| CN204469679U (en) | A kind of reaction system of organic oxygen compound catalytic cracking aromatic hydrocarbons | |
| CN105983452B (en) | A kind of regeneration method of organic oxide catalytic cracking arenes catalytic agent | |
| CN204469710U (en) | The regenerative system of a kind of organic oxygen compound catalytic cracking arenes catalytic agent |
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term | Granted publication date:20150715 |