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Número de publicaciónCN101306969 B
Tipo de publicaciónConcesión
Número de solicitudCN 200710040702
Fecha de publicación30 Nov 2011
Fecha de presentación16 May 2007
Fecha de prioridad16 May 2007
También publicado comoCN101306969A
Número de publicación200710040702.2, CN 101306969 B, CN 101306969B, CN 200710040702, CN-B-101306969, CN101306969 B, CN101306969B, CN200710040702, CN200710040702.2
Inventores忻晓琦, 王华文, 钟思青, 齐国祯
Solicitante中国石油化工股份有限公司, 中国石油化工股份有限公司上海石油化工研究院
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Enlaces externos:  SIPO, Espacenet
用于含氧化合物制低碳烯烃的反应装置 Reaction means for the oxygenate to olefins traducido del chino
CN 101306969 B
Resumen  traducido del chino
本发明涉及一种用于含氧化合物制低碳烯烃的反应装置,主要解决现有技术中装置生产能力低、低碳烯烃选择性低、催化剂循环量小、反应器温度梯度大的问题。 The present invention relates to an oxygenate to olefins reaction apparatus used, mainly to solve the prior art apparatus of low capacity, low selectivity of light olefins, a small catalyst circulation rate, reactor temperature gradient big problem. 本发明通过采用反应装置主要包括第一流化床反应器、第二流化床反应器和再生器,第一流化床反应器或第二流化床反应器均包括进料口1或13、出料口7、反应区2、沉降段4、汽提段3、旋风分离器5、气固快速分离装置16;第一流化床反应器汽提段3的底部和第二流化床反应器的反应区底部通过管线8相连;再生器包括再生区15、气固快速分离区17、再生器沉降段18、再生器汽提段24、再生器旋风分离器19;再生器底部开有再生介质入口14,再生区15上部设有气固快速分离装置17,再生器沉降段18内有旋风分离器19,顶部开有烟气出口20;第二流化床反应器汽提段3的底部和再生器的再生区15的底部通过管线12相连;再生器汽提段24的底部和第二流化床反应器反应区2的底部通过管线22相连的技术方案,较好地解决了该问题,可用于低碳烯烃的工业生产中。 The present invention uses a reaction apparatus including a first fluidized bed reactor, a second fluidized bed reactor and a regenerator, a first fluidized bed reactor or fluidized bed reactor comprises a second inlet 1 or 13 , the discharge port 7, the reaction zone 2, the settlement section 4, stripping section 3, a cyclone 5, rapid gas-solid separation means 16; bottom of the first fluidized bed reactor and the stripping section 3 of a second fluidized bed bottom of the reactor through line 8 is connected to the reaction zone; regenerator 15 includes a regeneration zone, rapid gas-solid separation zone 17, the regenerator 18 settling section, stripping section 24 the regenerator, the regenerator cyclone 19; bottom of the regenerator is opened regeneration medium inlet 14, the upper portion of the regeneration zone 15 has a gas-solid separation means 17 fast, the regenerator section 18 has a settling cyclone 19, the flue gas outlet 20 is opened at the top; a second fluidized bed reactor stripping zone 3 the bottom and the bottom of the regenerator 15 is connected to the regeneration zone through line 12; bottom of the regenerator bottom stripping section and a second reaction zone of the fluidized bed reactor 24 via line 22 coupled aspect, a better solution to the questions that can be used in industrial production of light olefins.
Reclamaciones(7)  traducido del chino
1. 一种用于含氧化合物制低碳烯烃的反应装置,反应装置主要包括第一流化床反应器、第二流化床反应器和再生器,第一流化床反应器或第二流化床反应器均包括进料口(1) 或(13)、出料口(7)、反应区(2)、沉降段(4)、汽提段(3)、旋风分离器(5)、气固快速分离装置(16);进料口(1)或(13)位于各自反应器底部,出料口(7)位于各自反应器上部;第一流化床反应器汽提段(3)的底部和第二流化床反应器的反应区底部通过管线(8)相连;再生器包括再生区(1¾、气固快速分离区(17)、再生器沉降段(18)、再生器汽提段04)、再生器旋风分离器(19);再生器底部开有再生介质入口(14),再生区(1¾上部设有气固快速分离装置(17),再生器沉降段(18)内有旋风分离器(19),顶部开有烟气出口OO);第二流化床反应器汽提段(3)的底部和再生器的再生区(1¾的底部通过管线(1¾相连;再生器汽提段04)的底部和第二流化床反应器反应区(2)的底部通过管线02)相连;其中,气固快速分离装置(16)位于各自流化床反应器反应区的上部,旋风分离器(5)位于各自流化床反应器沉降段的内部。 1. A reaction apparatus for oxygenates to olefins, the reaction means including a first fluidized bed reactor, a second fluidized bed reactor and a regenerator, a first or second fluidized bed reactor fluidized bed reactor comprises a feed port (1) or (13), the discharge port (7), the reaction zone (2), settling section (4), the stripping section (3), a cyclone (5) , rapid gas-solid separation means (16); feed port (1) or (13) at the bottom of each reactor, the discharge port (7) is located in the upper portion of each reactor; a first fluid bed reactor stripping zone (3 ) at the bottom of the bottom of the fluidized bed reactor and the second reaction zone (8 connected); regenerator comprises a regeneration zone (1¾, rapid gas-solid separation zone (17) through a line, the regenerator settling section (18), the regenerator steam stripping section 04), the regenerator cyclone (19); the bottom of the regenerator is opened regeneration medium inlet (14), the regeneration zone (1¾ Solid Separator upper portion provided with means (17), settling section of the regenerator (18) There cyclone (19), the top of the flue gas outlet opening OO); bottom bottom and a second regenerator fluidized bed reactor stripping section (3) of the regeneration zone (1¾ connected through line (1¾; regenerator the bottom of the stripping section 04) of the bottom of the fluidized bed reactor and the second reaction zone (2) is connected via line 02); wherein, rapid gas-solid separation means (16) located in the upper part of each reaction zone of a fluidized bed reactor, cyclone (5) is located inside the fluidized bed reactor are each settlement section.
2.根据权利要求1所述用于含氧化合物制低碳烯烃的反应装置,其特征在于第一流化床反应器、第二流化床反应器及再生器均为快速流化床。 2. The reaction apparatus 1 for oxygenates to olefins according to claim, wherein the first fluid bed reactor, a second fluidized bed reactor and regenerator are fast fluidized bed.
3.根据权利要求1所述用于含氧化合物制低碳烯烃的反应装置,其特征在于第二流化床反应器汽提段的底部和第一流化床反应器的反应区底部通过管线(9)相连。 3. The reaction apparatus 1 for oxygenates to olefins according to claim, characterized in that the bottom of the bottom of the second fluidized bed reactor stripping zone and a first reaction zone of a fluidized bed reactor via line (9) is connected.
4.根据权利要求1所述用于含氧化合物制低碳烯烃的反应装置,其特征在于再生器汽提段的底部和第一流化床反应器反应区的底部通过管线相连。 4. The reaction apparatus 1 for oxygenate to olefins according to claim, characterized in that the bottom of the reactor the reaction zone of the regenerator and the stripping section of the bottom of the first fluidized bed is connected by line.
5.根据权利要求1所述用于含氧化合物制低碳烯烃的反应装置,其特征在于第一流化床反应器汽提段的底部和再生器的再生区的底部通过管线0¾相连。 5. The reaction apparatus 1 for oxygenate to olefins according to claim, characterized in that the bottom and the bottom of the regenerator fluidized bed reactor of a first stripping zone of the regeneration zone is connected via line 0¾.
6.根据权利要求1所述用于含氧化合物制低碳烯烃的反应装置,其特征在于第一流化床反应器汽提段的底部和第一流化床反应器反应区的底部通过管线(10)相连;第二流化床反应器汽提段的底部和第二流化床反应器反应区的底部通过管线(11)相连。 6. The reaction apparatus 1 for oxygenates to olefins according to claim, characterized in that the bottom of the bottom of the first fluidized bed reactor and the first stripping zone the reaction zone of the fluidized bed reactor via line (10) is connected; bottom bottom and second fluid bed reactor the reaction zone of the reactor a fluidized bed stripping zone connected by a second line (11).
7.根据权利要求1所述用于含氧化合物制低碳烯烃的反应装置,其特征在于气固快速分离装置(16)的直径与第一流化床反应器或第二流化床反应器反应区O)的直径之比为0. 1〜0. 5 : 1 ;第一流化床反应器或第二流化床反应器内的旋风分离器(5)为1〜3级, 再生器沉降段(18)内的旋风分离器(19)为1〜3级。 7. The reaction apparatus 1 for oxygenates to olefins according to claim, characterized in that the diameter of the gas-solid separation means fast (16) with a first fluidized bed reactor or a second fluidized bed reactor The reaction zone O) than the diameter of 0. 1~0 5: 1; a first fluid bed reactor or the second reactor of the fluidized bed cyclone (5) is 1~3 stage regenerator. settling cyclone section (18) (19) for 1~3 level.
Descripción  traducido del chino

用于含氧化合物制低碳烯烃的反应装置 Reaction means for the oxygenate to olefins

技术领域 FIELD

[0001] 本发明涉及一种用于含氧化合物制低碳烯烃的反应装置。 [0001] The present invention relates to a reaction apparatus for the oxygen-containing compound to olefins. 背景技术 BACKGROUND

[0002] 低碳烯烃,主要是乙烯和丙烯,是两种重要的基础化工原料,其需求量在不断增加。 [0002] olefins, primarily ethylene and propylene, are two important basic chemical raw materials, the demand is increasing. 一般地,乙烯、丙烯是通过石油路线来生产,但由于石油资源有限的供应量及较高的价格,由石油资源生产乙烯、丙烯的成本不断增加。 Generally, ethylene, propylene is produced by the oil line, but because of the limited supply of petroleum resources and the higher the price, the cost of production of ethylene from petroleum resources, increasing propylene. 近年来,人们开始大力发展替代原料转化制乙烯、丙烯的技术。 In recent years, people began to develop alternative feedstock into ethylene, propylene technology. 其中,一类重要的用于低碳烯烃生产的替代原料是含氧化合物,例如醇类(甲醇、乙醇)、醚类(二甲醚、甲乙醚)、酯类(碳酸二甲酯、甲酸甲酯)等,这些含氧化合物可以通过煤、天然气、生物质等能源转化而来。 Among them, an important class of alternative raw materials for the production of light olefins are oxygenates, such as alcohols (methanol, ethanol), ethers (dimethyl ether, methyl ethyl ether), esters (dimethyl carbonate, methyl formate esters), these may be converted from an oxygen-containing compounds by coal, natural gas, biomass and other energy. 某些含氧化合物已经可以达到较大规模的生产,如甲醇,可以由煤或天然气制得,工艺十分成熟,可以实现上百万吨级的生产规模。 Certain oxygenates may have reached large-scale production, such as methanol, can be obtained from coal or natural gas, technology is very mature, you can achieve the megaton scale of production. 由于含氧化合物来源的广泛性,再加上转化生成低碳烯烃工艺的经济性,所以由含氧化合物转化制烯烃(OTO)的工艺,特别是由甲醇转化制烯烃(MTO)的工艺受到越来越多的重视。 Due to extensive source of oxygen-containing compounds, plus conversion of olefins to generate economic process, so-to-olefins (OTO) by oxygenate conversion process, in particular by the conversion of methanol to olefins (MTO) process more come more and more attention.

[0003] US4499327专利中对磷酸硅铝分子筛催化剂应用于甲醇转化制烯烃工艺进行了详细研究,认为SAP0-34是MTO工艺的首选催化剂。 [0003] US4499327 patent phosphate aluminosilicate zeolite catalysts for the conversion of methanol to olefins process carried out a detailed study, that is the preferred catalyst SAP0-34 MTO process.

[0004] US6166282中公布了一种氧化物转化为低碳烯烃的技术和反应器,采用快速流化床反应器,气相在气速较低的密相反应区反应完成后,上升到内径急速变小的快分区后,采用特殊的气固分离设备初步分离出大部分的夹带催化剂。 [0004] US6166282 discloses a in the conversion of oxygenates to light olefins and reactor technology, the use of a fast fluidized bed reactor, the gas velocity in the gas phase of the dense phase reaction zone lower the reaction was completed, up to the inner diameter of the rapid change After small fast partition, using a special gas-solid separation equipment initially isolated from most of the entrained catalyst. 由于反应后产物气与催化剂快速分离,有效的防止了二次反应的发生。 Since the reaction product gas after the rapid separation of the catalyst, is effective to prevent the occurrence of secondary reactions. 经模拟计算,与传统的鼓泡流化床反应器相比,该快速流化床反应器内径及催化剂所需藏量均大大减少。 After the simulation, compared with conventional bubbling fluidized bed reactor, the fast fluidized bed reactor volume required for possession diameter and catalyst greatly reduced. 但该方法所述的快速流化床反应器的单系列处理能力较低。 But lower fast fluidized bed reactor according to the method of the single series of processing capacity.

[0005] 另外,要保证高的低碳烯烃选择性,SAP0-34催化剂上需要积上一定量的碳。 [0005] In addition, to ensure a high selectivity to light olefins, you need a certain amount of carbon accumulated on SAP0-34 catalyst. US20060025646专利中涉及一种控制MTO反应器反应区中催化剂积炭量的方法,是将失活的催化剂一部分送入再生区烧炭,另一部分失活催化剂返回到反应区继续反应。 US20060025646 patent relates to a method for controlling the MTO reactor the catalyst in the reaction zone the amount of coke, which is partly deactivated catalyst into a regeneration zone by burning charcoal, another portion of the deactivated catalyst is returned to the reaction zone to continue the reaction. 由于MTO 工艺的剂醇比很小,生焦率较低,如果要在再生器内控制催化剂的烧炭程度,会使得反应器与再生器之间的催化剂流量较小,对催化剂流量控制的要求很高。 Because agents alcohol MTO process than a small, lower coke rate, if you want to control the extent of charcoal catalyst in the regenerator, will make the catalyst flow reactor and regenerator between small catalyst flow control requirements high.

[0006] 现有技术方法均存在装置生产能力低、再生器烧炭难以控制、催化剂循环量较小等方面的问题。 [0006] The apparatus of the prior art methods have problems of low productivity, the regenerator charcoal is difficult to control, the smaller the amount of catalyst circulation and other aspects exist.

发明内容 SUMMARY

[0007] 本发明所要解决的技术问题是现有技术中存在的装置生产能力低、低碳烯烃选择性低、催化剂循环量小、反应器温度梯度大的问题,提供一种新的用于含氧化合物制低碳烯烃的反应装置。 [0007] Technical Problem to be solved by the present invention is the production capacity of the prior art are low, the low selectivity of light olefins, a small catalyst circulation rate, reactor temperature gradient big problem, to provide a novel for containing oxy compounds made reaction apparatus light olefins. 该装置用于低碳烯烃的生产中,具有装置生产能力高、低碳烯烃选择性高、 催化剂循环量大、反应器温度梯度小的优点。 The apparatus for the production of light olefins having means high production capacity, high selectivity to light olefins, a large amount of catalyst cycle, the reactor temperature gradient small advantages.

[0008] 为解决上述问题,本发明采用的技术方案如下:一种用于含氧化合物制低碳烯烃 [0008] To solve the above problems, the present invention adopts the technical scheme is as follows: An oxygenate to olefins

3的反应装置,反应装置主要包括第一流化床反应器、第二流化床反应器和再生器,第一流化床反应器或第二流化床反应器均包括进料口1或13、出料口7、反应区2、沉降段4、汽提段3、旋风分离器5、气固快速分离装置16 ;进料口1或13位于各自反应器底部,出料口7位于各自反应器上部;第一流化床反应器汽提段3的底部和第二流化床反应器的反应区底部通过管线8相连;再生器包括再生区15、气固快速分离区17、再生器沉降段18、再生器汽提段对、再生器旋风分离器19 ;再生器底部开有再生介质入口14,再生区15上部设有气固快速分离装置17,再生器沉降段18内有旋风分离器19,顶部开有烟气出口20 ;第二流化床反应器汽提段3的底部和再生器的再生区15的底部通过管线12相连;再生器汽提段M的底部和第二流化床反应器反应区2的底部通过管线22相连。 The reaction apparatus, the reaction apparatus 3 mainly comprises a first fluid bed reactor, a second fluidized bed reactor and a regenerator, a first fluidized bed reactor or fluidized bed reactor comprises a second inlet 1 or 13, a gate 7, the reaction zone 2, paragraph 4 settlement, stripping section 3, 5 cyclone, rapid gas-solid separation means 16; inlet 1 or 13 at the bottom of each reactor, the discharge port is located 7 each top of the reactor; bottom of the first fluidized bed and second fluidized-bed reactor bottom reactor stripping zone 3 of the reaction zone is connected via line 8; regenerator 15 includes a regeneration zone, rapid gas-solid separation zone 17, the regenerator Section 18 settlement, stripping regenerator section right, regenerator cyclones 19; bottom of the regenerator opened regeneration medium inlet 14, the upper part of the regeneration zone 15 has a gas-solid separation means 17 fast regenerator settlement segment 18 has a cyclone 19, the top of the flue gas outlet 20 is opened; the bottom of the second bottom and the regenerator fluidized bed reactor stripping zone 3 is connected to the regeneration zone 15 through line 12; regenerator bottom of the stripping section and the second flow M the bottom of the fluidized bed reactor 2 is connected to the reaction zone through line 22.

[0009] 上述技术方案中,所述第一流化床反应器、第二流化床反应器及再生器均为快速流化床;第二流化床反应器汽提段的底部和第一流化床反应器的反应区底部通过管线9相连;再生器汽提段的底部和第一流化床反应器反应区的底部通过管线21相连;第一流化床反应器汽提段的底部和再生器的再生区的底部通过管线25相连;第一流化床反应器汽提段的底部和第一流化床反应器反应区的底部通过管线10相连;第二流化床反应器汽提段的底部和第二流化床反应器反应区的底部通过管线11相连;气固快速分离装置16位于各自流化床反应器反应区的上部;旋风分离器位于各自流化床反应器沉降段4的内部;气固快速分离装置16的直径与第一流化床反应器或第二流化床反应器反应区2的直径之比为0. 1〜0. 5 : 1 ;第一流化床反应器或第二流化床反应器内的旋风分离器5为1〜3级,再生器沉降段18内的旋风分离器19为1〜3级。 [0009] The above-mentioned modes, the first fluidized bed reactor, a second fluidized bed reactor and regenerator are fast fluidized bed; bottom of the second fluidized bed reactor and the first stripping zone the bottom of the fluidized bed reactor of the reaction zone is connected via line 9; the bottom of the reaction zone of the reactor regenerator and the stripping section of the bottom of the first fluidized bed is connected via line 21; the bottom of the first fluidized bed reactor stripping zone and the bottom of the regenerator is connected to the regeneration zone via line 25; the bottom of the reactor, the reaction zone of the first fluidized bed reactor and the bottom of the stripping section through the line 10 is connected to a first fluidized bed; second fluidized bed reactor vapor bottom of the reactor the reaction zone and the stripping section of the bottom of the second fluidized bed is connected via line 11; rapid gas-solid separation means 16 is located in the upper part of the respective fluidized-bed reactor reaction zone; cyclone located in the fluidized bed reactor are each Settlement interior section 4; Solid Separator diameter of the first fluidized bed reactor device 16 or the second fluid bed reactor diameter ratio of the reaction zone 2 is 0. 1~0 5: 1; the first flow bed reactor cyclone or a fluidized bed reactor in the second stage 5 is 1~3, the regenerator cyclone 18 within the settling section 19 for 1~3 level.

[0010] 由于甲醇分子量小,要达到上百万吨的甲醇处理规模所需的反应器体积相当大, 再加上甲醇转化为低碳烯烃反应过程中可能会加入一定量的稀释剂用以提高低碳烯烃的选择性,这样要达到一定的处理规模,所需的反应器直径会更大,而反应器直径的增大对于气固流动分布、内构件、返混控制等方面的要求会更高。 [0010] Due to the small molecular weight of methanol, to achieve the desired scale of hundreds of tons of methanol reactor volume is quite large, the conversion of methanol to light olefins during the reaction may be added together with a quantity of diluent to improve selectivity of light olefins, such treatment must reach a certain size, the required diameter of the reactor will be greater, while increasing the diameter of the reactor for the gas-solid flow distribution within the components, backmixing control and other requirements will be more high. 经计算,要实现100万吨/年的甲醇处理规模,单系列反应器的直径要达到10米以上。 Calculated to achieve scale methanol handle 1 million tons / year, a single series reactor to reach 10 meters or more in diameter. 直径这么大的反应器,会使得反应器内的气固流动分布不均勻,返混程度加大,由于MTO反应为强放热反应,因此还会使得反应器内的温度梯度加大,这些因素都将严重影响产品选择性。 Such a large diameter reactor, will make solid flow unevenly distributed within the reactor, increasing the degree of backmixing, MTO reaction due to strong exothermic reaction, but also makes the temperature gradient within the reactor increased, these factors will seriously affect the product selectivity. 另外,由于甲醇制烯烃反应的生焦率较低,而且还需要保证反应器内催化剂的平均积炭量在所需的水平上,造成反应-再生系统内的催化剂循环量很小,对催化剂流量的控制要求很高。 In addition, due to lower coke rate of methanol to olefins reaction, but also need to ensure that the average amount of carbon deposition reactor catalyst at the desired level, causing the reaction - the amount of regenerated catalyst circulation within the system is small, the catalyst flow control demanding. 本发明采用一种流化床反应器系统,设立两个流化床反应器,能够在单系列反应器直径较小的情况下实现较大的甲醇处理规模。 The present invention uses a fluidized bed reactor system, the establishment of two fluidized bed reactors, to achieve greater size of methanol in single series reactor diameter is small. 由于两个反应器之间催化剂的交换,使得整个反应系统内的催化剂积炭量调整更加灵活,在此基础上,可以提高再生器的烧炭强度,从而增大待生催化剂与再生催化剂的“碳差”,使得反应-再生系统内的催化剂循环量变大,流量控制更加容易。 Since the exchange between the two reactors the catalyst, so that the entire amount of the catalyst coke within the reaction system to adjust more flexible, based on this, the strength can be improved charcoal regenerator, thereby increasing the spent catalyst and regenerated catalyst " Carbon poor ", so that the reaction - catalyst recycling system becomes large, the flow control easier.

[0011] 采用本发明的技术方案:第二流化床反应器汽提段的底部和第一流化床反应器的反应区底部通过管线9相连;再生器汽提段的底部和第一流化床反应器反应区的底部通过管线21相连;第一流化床反应器汽提段的底部和再生器的再生区的底部通过管线25相连; 第一流化床反应器汽提段的底部和第一流化床反应器反应区的底部通过管线10相连;第二流化床反应器汽提段的底部和第二流化床反应器反应区的底部通过管线11相连;气固快速分离装置16位于各自流化床反应器反应区的上部;旋风分离器位于各自流化床反应器沉降段4的内部;气固快速分离装置16的直径与第一流化床反应器或第二流化床反应器反应区2的直径之比为0. 1〜0. 5:1 ;第一流化床反应器或第二流化床反应器内的旋风分离器5为1〜3级,再生器沉降段18内的旋风分离器19为1〜3级,低碳烯烃收率最高可达到77. 15% (重量),取得了较好的技术效果。 [0011] The aspect of the present invention: a first bottom of the second fluidized bed and the bottom of the fluidized bed reactor of a reactor stripping zone via line 9 is connected to the reaction zone; and a first flow regenerator bottom stripping section the bottom of the fluidized bed reactor the reaction zone is connected via line 21; and bottom part of the regenerator fluidized bed reactor of a first stripping zone of the regeneration zone through line 25 is connected; bottom of the first fluidized bed reactor stripping zone and the bottom of the first fluidized bed reactor is connected to the reaction zone via line 10; the bottom of the bottom of the fluidized bed reactor and a second reaction zone of the reactor a fluidized bed stripping zone connected by a second line 11; Solid Separator means the upper portion of the fluidized bed 16 is in its own reactor reaction zone; each cyclone located inside the fluidized bed reactor settling section 4; rapid gas-solid separation means 16 and the diameter of the first or second flow fluidized bed reactor diameter ratio of the reaction zone bed reactor 2 is 0.5 1~0 5: 1; a first fluidized bed reactor or inside the reactor cyclone 5 for 1~3 second stage fluidized bed, regeneration. the settling cyclone section 18 within 19 ~ 3 level, the highest yield of olefins can reach 77.15% (by weight), and achieved good technical results.

附图说明 Brief Description

[0012] 图1为本发明所述方法的流程示意图。 [0012] Figure 1 a schematic flow diagram of the method of the present invention.

[0013] 图1中,1为第一流化床反应器底部的进料管线;2为流化床反应器反应区;3为汽提段;4为流化床反应器的沉降段;5为反应器内旋风分离器;6为集气室;7为出料口;8 为第一流化床反应器向第二流化床反应器中输送催化剂的管线;9为第二流化床反应器向第一流化床反应器中输送催化剂的管线;10为第一流化床反应器汽提段催化剂返回反应区下部的输送管线;11为第二流化床反应器汽提段的催化剂返回反应区2下部的输送管线;12为第二流化床反应器中汽提后待生催化剂进入再生器的输送管线;13为第二流化床反应器底部的进料管线;14为再生器的进料口;15为再生器再生区;16为流化床反应器的气固快速分离段;17为再生器再生区上部的气固快速分离段;18为再生器沉降段;19为再生器内旋风分离器;20为烟气出口;21为再生催化剂返回第一流化床反应区的输送管线; 22为再生催化剂返回第二流化床反应区的输送管线;23为反应系统为再生催化剂汽提器;25为第一流化床反应器中汽提后待生催化剂进入再生器的输送管线。 [0013] Figure 1, 1 is the bottom of the first fluidized bed reactor feed line; 2 is a fluidized bed reactor the reaction zone; 3 is the stripping section; segment 4 for settling the fluidized bed reactor; 5 To the reactor cyclone; 6 plenum; 7 for the discharge port; 8 for a first fluidized bed reactor to the second fluidized bed reactor the catalyst transfer line; 9 for the second fluid bed transporting the reactor to a first fluidized-bed reactor the catalyst line; a first fluidized bed reactor 10 for the stripping section of the lower portion of the catalyst returned to the reaction zone transfer line; second fluidized bed reactor 11 for the stripping section The catalyst returned to the reaction zone of the lower part of the transfer line 2; 12 to the second fluidized-bed reactor after stripping spent catalyst transfer line to enter the regenerator; 13 feed line for the second fluid bed reactor bottom; 14 regenerator inlet; regenerator 15 for regeneration zone; 16 for the fluidized bed reactor Solid Separator segment; 17 is the upper portion of the regeneration zone of the regenerator rapid gas-solid separation section; settling section 18 for the regenerator; 19 within the regenerator cyclone; 20 for flue gas outlet; 21 returns the regenerated catalyst transfer line for the first fluidized bed reaction zone; 22 returns the regenerated catalyst transfer line for the second fluidized bed reaction zone; 23 for the reaction system to regenerated catalyst stripper; 25 for a first fluidized bed reactor and stripped spent catalyst transfer line to enter the regenerator.

[0014] 甲醇分别从进料管线1和13进入第一流化床反应器和第二流化床反应器的反应区2,与催化剂接触生成含催化剂粉尘、乙烯、丙烯的物流,分别经各自反应器沉降段4中的旋风分离器5分离后,含乙烯、丙烯的气相从各自反应器顶部进入集气室6,从集气室6顶部的出口7排出进入后续的分离工段,分离出的催化剂粉尘沉降或从各自旋风分离器5下部的催化剂料腿返回各自流化床反应器沉降段4下部的汽提段3,经汽提后一部分催化剂通过管线12或25进入再生器再生区15底部,一部分催化剂通过管线8、9进入另一流化床反应器的底部,一部分催化剂通过管线10、11返回各自流化床反应器下部的反应区2。 [0014] methanol 2 respectively, generated dust containing catalyst, ethylene, propylene stream from a feed line 1 and 13 into the first fluidized bed reactor and the second reaction zone of a fluidized bed reactor in contact with the catalyst, respectively, via respective The reactor settling section 4 after the separation cyclone 5, comprising ethylene, propylene gas phase enters the reactor from the top of each plenum chamber 6, is discharged from the outlet 6 at the top of the gas collection chamber 7 into the subsequent separation section, separated The catalyst settling dust or return to their respective fluidized bed reactor from a lower portion of the cyclone 5 dipleg catalyst settling fourth lower section of the stripping section 3, after the stripped portion of the catalyst 15 through the bottom line 12 or 25 into the regenerator the regeneration zone , another portion of the catalyst into the bottom of the fluidized bed reactor through line 8 and 9, each portion of the catalyst to return the lower portion of a fluidized bed reactor the reaction zone 2 via line 10, 11. 待再生的催化剂经再生器再生、汽提器M汽提后,一部分催化剂通过管线21返回第一流化床反应器下部反应区,一部分催化剂通过管线22返回第二流化床反应器下部反应区,生成的烟气经过再生器内的旋风分离器19分离后由烟气出口20排出。 The catalyst to be regenerated by the regenerator the regeneration, after stripping stripper M, a first portion of the catalyst to return the lower portion of the fluidized bed reactor the reaction zone via line 21, a second portion of the catalyst to return the lower portion of the fluidized bed reactor the reaction zone through line 22 the resulting flue gas through the regenerator cyclones within 19 after separation is discharged from the flue gas outlet 20.

[0015] 下面通过实施例对本发明作进一步的阐述,但不仅限于本实施例。 [0015] The following examples of the present invention is further illustrated by, but is not limited to this embodiment.

具体实施方式 DETAILED DESCRIPTION

[0016]【实施例1〜4】 [0016] [Example 1 ~ 4]

[0017] 在如图1所示的反应-再生装置中,再生器采用快速流化床,提升气体为空气,再生温度600°C。 [0017] In the reaction shown in Figure 1 - reproducing apparatus, a fluidized bed regenerator with fast, lift gas is air, the regeneration temperature of 600 ° C. 两个反应器均采用快速流化床,每个反应器内的气体表观速度均为1.2米/ 秒,反应温度为425°C,纯甲醇进料,其中40% (重量)进入第一流化床反应器,甲醇重量空速均为3小时―1,以表压计反应和再生压力均为OMPa。 Two reactors are used in a fast fluidized bed, the superficial gas velocity in each reactor are 1.2 m / sec, the reaction temperature was 425 ° C, pure methanol feed, of which 40% (by weight) into the first flow bed reactor, the methanol WHSV was 3 h-1, the reaction gauge pressure and regeneration pressure are OMPa. 第一流化床反应器汽提段通过管线8与第二流化床反应器反应区相连,催化剂流量与管线25、10中的催化剂流量的重量比为1:2:3。 The first fluid bed reactor stripping zone via line 8 connected to the second fluidized bed reactor the reaction zone, the weight of the catalyst flow and catalyst flow lines 25,10 in the ratio of 1: 2: 3. 第二流化床反应器汽提段通过管线9与第一流化床反应器反应区相连,催化剂流量与管线12、11中的催化剂流量的重量比为1 : 2 : 3。 The second fluidized bed reactor stripping zone via line 9 is connected to the first fluid bed reactor the reaction zone, the weight of catalyst flow and the flow line 12, 11 in the ratio of catalyst 1: 2: 3. 气固快速分离装置16位于各自流化床反应器反应区的上部,旋风分离器位于各自流化床反应器沉降段4的内部;气固快速分离装置16的直径与第一流化床反应器或第二流化床反应器反应区2的直径之比为0.12:1 ;第一流化床反应器或第二流化床反应器内的旋风分离器5为1级。 Rapid gas-solid separation means 16 is in its own upper portion of the fluidized bed reactor, the reaction zone, the cyclone located in the fluidized bed reactor settling each interior section 4; Solid Separator diameter of the first fluidized bed reactor device 16 diameter ratio of the second fluidized-bed reactor or reaction zone 2 is 0.12: 1; a first fluidized bed reactor or inside the reactor cyclone 5 is a second fluidized bed. 再生器沉降段18内的旋风分离器19为1级。 Settlement of the regenerator section within the cyclone 18 to a 19. 再生剂和待生剂的取样口分别位于管线21和管线12上,催化剂上碳含量的分析采用红外碳硫高速分析仪。 Spent catalyst regeneration agents and sampling ports are located on the line 21 and line 12, the analysis on the carbon content of the catalyst using the high-speed infrared carbon and sulfur analyzer. 将催化剂的循环量保持在一个合理的值, 使得系统运行稳定、控制方便,催化剂循环量与甲醇总进料质量流量之比为2。 The catalyst circulation is maintained at a reasonable value, making the system is stable, easy to control, and the methanol catalyst circulation total mass flow rate of feed intake than two. 催化剂采用经喷雾干燥成型的SAP0-34改性催化剂。 Use of spray-dried catalyst formed SAP0-34 reforming catalyst. 反应器出口产物采用在线气相色谱分析,实验结果见表1。 Reactor outlet product using online gas chromatographic analysis of the experimental results shown in Table 1.

[0018] 表1 [0018] Table 1

[0019] [0019]

Figure CN101306969BD00071

[0020]【实施例5】 [0020] [Example 5]

[0021] 按照实施例2所述的条件,改变气固快速分离装置16的直径与第一流化床反应器或第二流化床反应器反应区2的直径之比为0. 5 : 1 ;第一流化床反应器或第二流化床反应器内的旋风分离器5为3级。 [0021] according to the conditions described in Example 2, the ratio of the diameter of Solid Separator change the diameter of the first fluidized bed reactor device 16 or the second reaction zone of a fluidized bed reactor 2 is 0.5: 1 ; first fluid bed reactor or the second fluid bed reactor cyclone 5 for three. 再生器沉降段18内的旋风分离器19为3级,实验结果为:乙烯碳基收率为39. 97 % (重量),丙烯碳基收率为37. 18 % (重量),乙烯+丙烯碳基收率为77. 15% (重量)。 Regenerator settling section 18 inside the cyclone 19 is 3, the experimental results: carbon-based ethylene yield 39.97% (by weight), propylene-carbon-based yield 37.18% (by weight), ethylene + propylene The carbon-based yield 77.15% (by weight).

Citas de patentes
Patente citada Fecha de presentación Fecha de publicación Solicitante Título
CN1723262A22 Ago 200318 Ene 2006埃克森美孚化学专利公司Multiple riser reactor with centralized catalyst return
US616628220 Ago 199926 Dic 2000Uop LlcFast-fluidized bed reactor for MTO process
Clasificaciones
Clasificación internacionalC07C1/20, C07C11/02, B01J8/26
Eventos legales
FechaCódigoEventoDescripción
19 Nov 2008C06Publication
14 Ene 2009C10Request of examination as to substance
30 Nov 2011C14Granted