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CN101306969B - The reaction apparatus for an oxygenate to light olefins - Google Patents

The reaction apparatus for an oxygenate to light olefins Download PDF

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CN101306969B
CN101306969B CN 200710040702 CN200710040702A CN101306969B CN 101306969 B CN101306969 B CN 101306969B CN 200710040702 CN200710040702 CN 200710040702 CN 200710040702 A CN200710040702 A CN 200710040702A CN 101306969 B CN101306969 B CN 101306969B
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CN 200710040702
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CN101306969A (en )
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忻晓琦
王华文
钟思青
齐国祯
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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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Abstract

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 a reactor an oxygenate to light olefins is used, mainly to solve the prior art apparatus of low capacity, low selectivity to light olefins, a small amount of catalyst circulation, reactor temperature gradient large. 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。 By using the reaction apparatus of the present invention 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 13 or 1 , the discharge port 7, the reaction zone 2, a settling 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 second fluidized bed bottom of the reaction zone of the reactor through line 8 is connected; regenerator 15 includes a regeneration zone, Solid separator zone 17, the regenerator settling section 18, the stripping section of the regenerator 24, the regenerator cyclone 19; bottom of the regenerator is opened regeneration medium inlet 14, upper regeneration zone 15 is provided with a gas-solid separation means 17 fast with the regenerator cyclone 19 within the settling section 18, a top flue gas outlet opening 20; second fluidized bed reactor stripping section 3 the bottom of the regeneration zone and the bottom of the regenerator 15 is connected through line 12; and bottom of the second fluidized-bed reactor bottom the reaction zone regenerator 2 stripper section 24 via line 22 coupled aspect, a better solution to the problem, can be used in industrial production of light olefins.

Description

用于含氧化合物制低碳烯烃的反应装置 The reaction apparatus for an oxygenate to light 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 an oxygenate to light olefins is provided. 背景技术 Background technique

[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] The light olefins, mainly 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 are produced by the oil route, but due to limited supply of petroleum resources and the higher the price, the cost of production of ethylene from petroleum resources, increasing the 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 technologies feedstock into ethylene, propylene. 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。 Wherein, 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 oxygenate 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 have large-scale production can be achieved, such as methanol, may be obtained from coal or natural gas, very mature technology, can be implemented on a production scale megaton. 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。 Because of the extensive source oxygenate, together with conversion of olefins to generate economic process, so the process to olefins (the OTO) conversion of the oxygenates, in particular by the conversion of methanol to olefins (MTO) process more to 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 applied for the conversion of methanol to olefins process silicoaluminophosphate zeolite catalysts were studied in detail, the preferred catalyst SAP0-34 that the 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 the conversion of oxygenates to light olefins and reactor technology, the use of a fast fluidized bed reactor, after completion of the reaction gas in the lower gas velocity dense phase reaction zone, rising to rapidly change the inner diameter fast after a small partition, gas-solid separation apparatus using special preliminary separation of the majority of 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, effectively prevents 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。 Simulated calculation, compared with the conventional bubbling fluidized bed reactor, a fast fluidized bed of the desired inner diameter of the reactor volume and catalyst inventory is 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 power.

[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] Further, to ensure a high selectivity to light olefins, you need a certain amount of carbon accumulated on the catalyst SAP0-34. 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。 Patent US20060025646 relates to a method for the MTO reactor the amount of catalyst coke in the control reaction zone, which is partially deactivated catalyst into a regeneration zone by burning charcoal, another portion of the deactivated catalyst is returned to the reaction zone the reaction was continued. 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。 Since the MTO process alcohol agent, a lower rate than small coke, charcoal To control the degree of catalyst in the regenerator, the catalyst flow will be so small between the reactor and regenerator, the 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 method of the prior art devices have a problem of low productivity, the regenerator charcoal is difficult to control, the smaller the amount of catalyst and other aspects of the present cycle.

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] The present invention solves the technical problem present in the prior art of low production capacity of the device, a low selectivity to light olefins, a small amount of catalyst circulation, reactor temperature gradient big problem, to provide for a novel containing oxides of olefins reactor system. 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 production of light olefins, the apparatus having a high production capacity, high selectivity to light olefins, the catalyst circulation amount, reactor temperature gradient is 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] In order to solve the above problems, the present invention employs the following technical solution: an oxygen-containing compound to light 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 device 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 feed port or 1 13, the discharge port 7, the reaction zone 2, a settling section 4, stripping section 3, a cyclone 5, rapid gas-solid separation means 16; 1 or inlet 13 located at each bottom of the reactor, located in a respective discharge port 7 an upper portion of the reactor; the bottom of the first fluidized bed reaction zone and a second fluidized-bed reactor bottom stripping section 3 connected to the reactor through line 8; the regenerator 15 includes a regeneration zone, Solid separator zone 17, the regenerator settling section 18, the regenerator stripping segment pair, the regenerator cyclone 19; bottom of the regenerator regeneration medium inlet 14 is opened, the upper portion of the regeneration zone 15 is provided with a gas-solid separation means 17 fast with the regenerator cyclone settling section 18 19, a flue gas outlet 20 is opened at the top; bottom and the bottom of the regeneration zone of the regenerator of the second fluidized bed reactor 15 stripping section 3 is connected via line 12; the 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 [0009] In the above aspect, the first fluidized bed reactor, and a second fluidized bed reactor are a fast fluidized bed regenerator; reactor bottom stripping section of the first and second fluidized bed the bottom of the reaction zone of the fluidized bed reactor through line 9 is connected; bottom of the regenerator and the stripping section of the bottom of the first fluidized bed reactor is connected to the reaction zone via line 21; the bottom of the reactor, a first fluidized bed stripping section and the bottom of the regeneration zone is connected to the regenerator through line 25; and bottom of the bottom of the first reaction zone of the fluidized bed reactor a first fluid bed reactor stripping section is connected through line 10; a second fluidized bed reactor vapor and a bottom stripping section of the bottom of the second fluidized bed reactor the reaction zone is connected via line 11; Solid separator means 16 are each located in an upper portion of the fluidized bed reactor of the reaction zone; cyclone located in a respective fluid bed reactor settling inner section 4; Solid separator diameter of the first fluidized bed reactor device 16 or the second reaction zone is a fluidized bed reactor diameter ratio of 0.5 1~0 2 5: 1; a first flow cyclone in a second bed reactor or fluidized bed reactor 5为1〜3级,再生器沉降段18内的旋风分离器19为1〜3级。 5 ~ 3 stage cyclone separator 18 in the settling section 19 of the regenerator 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 methanol, to achieve the desired scale of hundreds of tons of methanol reactor rather bulky, plus the conversion of methanol to light olefins during the reaction may be added to increase the amount of diluent a selective to light olefins, and a process to reach a certain size, will be required for larger reactor diameter, reactor diameter is increased for the distribution of gas-solid flow, the inner member, backmixing control and other aspects 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 methanol 1 million tons / year, the diameter of a single series of reactors to reach 10 meters. 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, to increase the degree of backmixing, due to the highly exothermic MTO reaction is therefore also such that the temperature gradient in the reactor is 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。 Further, due to the lower coke reaction of methanol to olefins, but also need to ensure that the average amount of coke in the reactor the catalyst at the desired level, causing the reaction - regeneration of the catalyst circulation within the system is small, the flow rate of the catalyst 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, can be achieved in large scale single methanol reactor series diameter is smaller. 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 amount of catalyst coke in the entire reaction system is more flexible to adjust, based on this, the strength can be improved charcoal regenerator, thereby increasing the spent catalyst and the regenerated catalyst " carbon difference ", so the reaction - regeneration of the catalyst circulation within the 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 [0011] The technical solution of the present invention: the bottom of the reaction zone and the bottom of the second fluidized bed reactor, a first reactor of the stripping section is connected via line 9; and a first flow regenerator bottom stripping section the bottom of the reaction bed zone of the reactor is connected by a line 21; the bottom of the regeneration zone and the bottom of the regenerator fluidized bed reactor a first stripping section is connected by a line 25; the bottom of the reactor, a first fluidized bed stripping section and the bottom of the first fluidized bed reactor the reaction zone is connected via line 10; and bottom of the second fluidized-bed reactor bottom the reaction zone of the reactor a fluidized bed stripping section are connected by a second line 11; Solid separator means 16 located in a respective upper fluidized bed reactor of the reaction zone; each cyclone located inside the fluidized bed reactor settling section 4; Solid separator diameter of the first fluidized bed reactor 16 or the second flow means diameter ratio of the reaction zone of the reactor bed 2 is 1~0 0. 5: 1; a first cyclone or a fluidized bed reactor in the reactor bed 5 to a second level 1~3 regeneration. the settling section 18 of the inner cyclone 19 1~3 stage, olefins yield 率最高可达到77. 15% (重量),取得了较好的技术效果。 It could be up to 77.15% (by weight), and achieved good results in the art.

附图说明 BRIEF DESCRIPTION

[0012] 图1为本发明所述方法的流程示意图。 [0012] Fig 1 a schematic flow chart 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 In [0013] FIG. 1, 1 is the bottom of the first fluidized bed reactor feed line; reactor 2 is a fluidized bed reaction zone; stripping section 3; 4 is a fluidized bed reactor settling section; 5 is a cyclone reactor; 6 plenum; is a discharge opening 7; 8 as a first fluid bed reactor catalyst transport line to the second fluidized-bed reactor; 9 is a second fluidized bed reactor catalyst transport line to a first fluidized bed reactor; a first fluidized bed reactor 10 is a stripping section of the lower portion of the catalyst returned to the reaction zone of the transport line; second fluidized bed reactor 11 stripping section the catalyst returned to the reaction zone a lower transfer line 2; 12 is a spent catalyst entering the regenerator fluidized bed reactor after the second stripping the transfer line; second fluidized bed 13 to the feed line at the bottom of the reactor; 14 inlet regenerator; regeneration zone 15 to the regenerator; a fluidized bed reactor 16 rapid gas-solid separation section; upper portion of the regenerator 17 to the regeneration zone Solid separator segments; settling section 18 of the regenerator; 19 the fluidized bed reactor 21 is returned to the first regenerated catalyst; within the regenerator cyclones; flue gas outlet 20 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。 Transfer line region; regenerated catalyst return conveyor 22 for the second line of the fluidized bed reaction zone; the reaction system is 23 to regenerated catalyst stripper; 25 after a first fluid bed reactor stripped spent catalyst to the regenerator 's transfer line.

[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, respectively 2, catalyst is contacted with the catalyst containing stream to generate dust, ethylene, propylene and 1 from the feed line 13 into the first fluidized bed reactor and the second reaction zone of the fluidized bed reactor, respectively, via respective after settling in the reactor section 5 separating cyclone 4, containing ethylene, propylene gas phase enters the reactor from the top of each plenum chamber 6, the discharge outlet 6 at the top of the plenum into the chamber 7 from the subsequent separation stage, separated the catalyst dust deposition or fluidized bed reactor to return to their settling section stripping section 4 from the lower portion of each cyclone dipleg catalyst 5 of the lower portion 3, the stripped portion of the catalyst through the bottom line 12 or 25 into the regeneration zone the regenerator 15 , a further portion of the catalyst into the bottom of the fluidized bed reactor through line 8 and 9, each portion of the catalyst returned to the reaction zone of a lower portion of a fluidized bed reactor 2 via line 10 and 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。 Regenerated catalyst to be regenerated by the regenerator, is stripped stripped M, returns to the first portion of the catalyst fluidized bed reactor lower reaction zone via line 21, returns to the second portion of the catalyst fluidized bed reactor lower reaction zone 22 via line generating flue gas through the regenerator in cyclone separator 19 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 will be 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 fast fluidized bed reactors are used, the gas superficial 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 hr⁻¹, a 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 stripper section is connected to the second fluidized bed reactor, the reaction zone via line 8, the weight of the catalyst flow and catalyst flow line 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 section connected to the first reaction zone of the fluidized bed reactor via line 9, the weight of the catalyst flow and catalyst flow line 12, 11 in the ratio of 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。 Solid Separator means 16 are each located in an 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 a reaction zone 2 is 0.12: 1; a first cyclone or a fluidized bed reactor in a second fluidized-bed reactor 5 1 grade. 再生器沉降段18内的旋风分离器19为1级。 18 in the regenerator cyclone settling section 19 of stage 1. 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。 Regenerated catalyst and spent catalyst sampling port are located on the line 21 and line 12, the carbon content analysis of the catalyst using a 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 amount of the circulating catalyst is maintained at a reasonable value, such that the system is stable, easy to control, and the methanol catalyst circulation ratio of the total mass flow rate of material into 2. 催化剂采用经喷雾干燥成型的SAP0-34改性催化剂。 The catalyst was dried using a modified catalyst SAP0-34 shaped spray. 反应器出口产物采用在线气相色谱分析,实验结果见表1。 The reactor outlet products 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] under the conditions described in Example 2, changing Solid Separator diameter ratio of the diameter of the first fluidized bed reactor device 16 or the second reaction zone is a fluidized bed reactor 2 is 0.5: 1 ; a first fluidized bed reactor or a fluidized bed cyclone 5 in the second reactor stage 3. 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)。 The regenerator cyclone in the settling section 1819 is level 3, the experimental results: the carbon-based ethylene yield was 39.97% (by weight), propylene-based carbon yield 37.18% (by weight), ethylene + propylene carbon-based yield 77.15% (by weight).

Claims (7)

  1. 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 A reaction apparatus oxygenates to light olefins used for the reaction apparatus including a first fluidized bed reactor, a second fluidized bed reactor and a regenerator, a first or second fluidized bed reactor the fluidized bed reactor includes a feed port (1) or (13), the discharge port (7), a reaction zone (2), settling section (4), stripping section (3), a cyclone (5) , rapid gas-solid separation means (16); a feed inlet (1) or (13) located at each bottom of the reactor, the discharge port (7) located at the upper portion of each reactor; a first fluidized bed reactor stripping section (3 ) and the bottom of the reaction zone at the bottom of the second fluidized bed reactor (8 connected); regeneration zone comprises a regenerator (1¾, rapid gas-solid separation zone (17) through line, the regenerator settling section (18), steam regenerator 04), the regenerator cyclone stripper section (19); the bottom of the regenerator is opened regeneration medium inlet (14), the regeneration zone (upper portion with 1¾ Solid separator device (17), settling section of the regenerator (18) there cyclone (19), a top flue gas outlet opening OO); the bottom of the regeneration zone (3) and the bottom of the regenerator fluidized bed reactor of the second stripping section (1¾ of 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。 Through line (1¾ connected; regenerator stripping section 04) and the bottom of the second fluidized-bed reactor bottom the reaction zone (2) is connected through line 02); wherein Solid Separator means (16) located in a respective fluidizing an upper portion of the reaction bed zone of the reactor, cyclone (5) is located inside the fluidized bed reactor are each settling section.
  2. 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 for an oxygenate to light olefins according to the claim 1, characterized in that the first fluidized bed reactor, and a second fluidized bed reactor are a fast fluidized bed regenerator.
  3. 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. A reaction apparatus for an oxygenate to light olefins according to the claim 1, characterized in that the bottom of the reaction zone at the bottom of the second fluidized bed reactor stripping section and a first fluidized bed reactor through line (9) is connected.
  4. 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 reactor apparatus for an oxygenate to light olefins in the claim 1, characterized in that the bottom of the regenerator and the stripping section of the bottom of the first fluidized bed reactor via line connected to the reaction zone.
  5. 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。 The reaction apparatus for an oxygenate to light olefins according to the claim 1, characterized in that the bottom and the bottom of the regeneration zone of the regenerator fluidized bed reactor a first stripping section is connected through line 0¾.
  6. 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. A reaction apparatus for an oxygenate to light olefins according to the claim 1, characterized in that the bottom of the bottom of the first fluidized bed reactor and the stripping section of the first reaction zone is a fluidized bed reactor via line (10) is connected; bottom bottom and a second fluidized bed reactor the reaction zone of the reactor a fluidized bed stripping section are connected by a second line (11).
  7. 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. A reaction apparatus for an oxygenate to light olefins according to the claim 1, characterized in that the diameter of Solid Separator device (16) with a first fluidized bed reactor or a second fluidized bed reactor the reaction zone O) ratio of the diameter of 1~0 0. 5: 1; fluidized bed reactor or a first cyclone (5) in a second fluidized bed reactor is 1~3 stage regenerator. cyclone (19) in the settling section (18) is 1~3 level.
CN 200710040702 2007-05-16 2007-05-16 The reaction apparatus for an oxygenate to light olefins CN101306969B (en)

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