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CN104672045A - Reaction device for preparing low-carbon olefin by employing methyl alcohol and/or dimethyl ether - Google Patents

Reaction device for preparing low-carbon olefin by employing methyl alcohol and/or dimethyl ether Download PDF

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CN104672045A
CN104672045A CN 201310648651 CN201310648651A CN104672045A CN 104672045 A CN104672045 A CN 104672045A CN 201310648651 CN201310648651 CN 201310648651 CN 201310648651 A CN201310648651 A CN 201310648651A CN 104672045 A CN104672045 A CN 104672045A
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reaction
carbon
device
low
fluidized
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CN 201310648651
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CN104672045B (en )
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张涛
叶茂
刘中民
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中国科学院大连化学物理研究所
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    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00Technologies relating to oil refining and petrochemical industry
    • Y02P30/40Ethylene production
    • Y02P30/42Ethylene production using bio-feedstock

Abstract

The invention relates to a reaction device for preparing low-carbon olefin by employing methyl alcohol and/or dimethyl ether, in particular to a reaction device for preparing low-carbon olefin by employing methyl alcohol and/or dimethyl ether. The reaction device mainly comprises a dense-phase fluidized bed reactor (2), a cyclone separator (3), a stripper (5), a lift pipe (7), a dense-phase fluidized bed regenerator (10), a cyclone separator (11), a stripper (13) and a lift pipe (15), wherein the dense-phase fluidized bed reactor (2) is partitioned into n (n is greater than or equal to 2) secondary reaction zones by material flow controllers (17); and the dense-phase fluidized bed regenerator (10) is partitioned into m (m is greater than or equal to 2) secondary regeneration zones by the material flow controllers (17). By virtue of the reaction device, the problems in the prior art that carbon deposit distribution of a catalyst is uneven and low-carbon olefin selectivity is relatively low are solved.

Description

—种用于甲醇和/或二甲醚制低碳烯烃的反应装置 - a kind of reaction apparatus methanol and / or dimethyl ether to light olefins

技术领域 FIELD

[0001] 本发明涉及一种用于甲醇和/或二甲醚制低碳烯烃的反应装置。 [0001] The present invention relates to a methanol and / or dimethyl ether the reaction apparatus for olefins.

背景技术 Background technique

[0002] 低碳烯烃,即乙烯和丙烯,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, i.e. 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. 甲醇转化制烯烃(MTO)的工艺受到越来越多的重视,已实现百万吨级的生产规模。 Methanol conversion process to olefins (MTO) is receiving more and more attention has been achieved megaton scale of production. 随着世界经济的发展,低碳烯烃,特别是丙烯,需求量与日俱增,析迈公司(CMAI)分析称,在2016年前,乙烯需求量将以年均4.3%的速度增长,丙烯需求量将以年均4.4%的速度增长。 As the world economy, light olefins, particularly propylene, increasing demand, analysis step the company (CMAI) analysis said that in 2016, ethylene demand will average 4.3% growth rate, the demand for propylene average annual growth rate of 4.4%. 由于我国经济的高速增长,我国乙烯和丙烯的需求量的年增长率均超过世界平均水平。 Due to China's rapid economic growth, the annual growth rate of demand for ethylene and propylene our country more than the world average.

[0003] 20世纪80年代初,UCC公司成功开发出了SAPO系列分子筛,其中SAP0-34分子筛催化剂在用于MTO反应时表现出优异的催化性能,具有很高的低碳烯烃选择性,而且活性很高,但催化剂在使用一段时间后由于积碳而失去活性。 [0003] In the early 1980s, the UCC has successfully developed a series of SAPO molecular sieves, wherein the molecular sieve catalyst SAP0-34 exhibits excellent catalytic performance when used for MTO reaction, the light olefins with high selectivity and activity high, but the catalyst in use for some time due to the carbon and loss of activity. SAP0-34分子筛催化剂在使用过程中存在明显的诱导期,在诱导期内,烯烃的选择性较低,烷烃的选择性较高,随着反应时间的增加,低碳烯烃选择性逐渐上升,诱导期过后,催化剂在一定时间内保持高的选择性和高的活性,随着时间的继续延长,催化剂的活性迅速下降。 SAP0-34 presence of a molecular sieve catalyst induction period was apparent during use, in the induction phase, low selectivity to olefins, higher alkanes selectivity with increasing reaction time, selectivity to light olefins gradually increased, induced after the period, the catalyst maintained a high selectivity and high activity over time, with the continued extension of time, the activity of the catalyst decreases rapidly.

[0004] US6166282中公布了一种甲醇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 methanol to light olefins and reactor technology, the use of a fast fluidized bed reactor, the gas phase after completion of the reaction gas velocity in the lower dense phase reaction zone, rising rapidly becomes smaller inner diameter after partition fast, special gas-solid separation apparatus of the 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. 但该方法中低碳烯烃碳基收率一般均在77 %左右,存在低碳烯烃收率较低的问题。 However, the yield of the carbon-based lower olefins process generally about 77%, there is a problem of low yield of light olefins.

[0005] CN101402538B公布了一种提高低碳烯烃收率的方法,该方法采用在甲醇转化为低碳烯烃的第一反应区上部设置一个第二反应区,且该第二反应区直径大于第一反应区,以增加第一反应区出口的产品气体在第二反应区内的停留时间,使得未反应的甲醇、生成的二甲醚和碳四以上烃继续反应,达到提高低碳烯烃收率的目的,该方法虽然可以在一定程度上提高低碳烯烃的收率,但是由于第一反应区出来的催化剂已经带有较多的积碳,而碳四以上烃裂解需要较高的催化剂活性,因此该方法中第二反应区内的碳四以上烃转化效率仍然偏低,从而导致低碳烯烃收率偏低。 [0005] CN101402538B discloses a method to improve the yield of light olefins, the method employed in the conversion of methanol to light olefins in a first reaction zone a second upper portion disposed reaction zone, and the second diameter is greater than the first reaction zone the reaction zone to increase product outlet of the first reaction zone residence time of the gas in the second reaction zone, such unreacted methanol, dimethyl ether and the resulting four or more carbon hydrocarbons reaction was continued, to improve the yield of light olefins object, although this method can improve the yield of light olefins to some extent, but since the first zone out of the reaction with catalysts have been more carbon, but more than four carbon hydrocarbon pyrolysis requires high catalyst activity, thus the process of the second reaction zone carbon four or more hydrocarbon conversion efficiency is still low, resulting in low yield of light olefins.

[0006] CN102276406A公布了一种增产丙烯的生产方法。 [0006] CN102276406A published method of producing a yield of propylene. 该技术设置三个反应区,第一快速床反应区用于甲醇转化至烯烃,提升管反应区和第二快速床反应区串联用于转化乙烯、碳四以上烃和未反应的甲醇或二甲醚。 This technique provided three reaction zones, the first reaction bed zone for rapid conversion of methanol to olefins, the riser reaction zone and a second reaction zone in series fast bed for conversion of methanol or dimethyl ethylene, four or more carbon hydrocarbons and unreacted ether. 此专利中碳四以上烃等物质在提升管反应区和第二快速床反应区中的停留时间较短,转化效率偏低,从而导致丙烯收率偏低。 In this patent carbon four or more substances such as a hydrocarbon residence time in the riser reaction zone and the second reaction zone of rapid short bed, low conversion efficiency, resulting in low yield of propylene.

[0007] CN102875289A公布了一种内部布置提升管反应器的流化床反应装置,用于提高低碳烯烃的产率。 [0007] CN102875289A published fluidized-bed reactor an internal arrangement of the riser reactor for increasing the yield of light olefins. 第一原料进入流化床反应区,与催化剂接触,生成包括低碳烯烃的产品,同时形成待生催化剂;待生催化剂一部分进入再生器再生,形成再生催化剂,一部分进入出口端位于反应区内部的提升管,与第二原料接触,将待生催化剂提升至反应区内;再生催化剂返回流化床反应器反应区。 First raw material into the fluidized bed reaction zone into contact with the catalyst to produce light olefins comprising the product, while forming a spent catalyst; spent catalyst entering the regenerator portion of the regeneration, the regenerated catalyst is formed, into the outlet end portion located inside the reaction zone riser, a second material in contact with the spent catalyst to enhance the reaction zone; regenerated catalyst is returned fluidized bed reactor the reaction zone. 此专利所披露的反应装置无汽提部分,待生催化剂将会携带部分产品气体进入再生器,与氧气发生燃烧,降低低碳烯烃的产量。 The reaction apparatus disclosed in this patent no steam stripping section, will carry the spent catalyst entering the regenerator portion of the product gas, oxygen and combustion occurs, reducing the yield of light olefins.

[0008] CN102875296A公布的甲醇制烯烃技术设置了快速床、下行床和提升管三个反应区。 [0008] CN102875296A published MTO technology is provided a fast bed, riser and downer three reaction zones. 催化剂在再生器、快速床、提升管和下行床之间循环,流向十分复杂、流量分配和控制十分困难,催化剂的活性变化较大。 The catalyst in the regenerator, fast bed, improve circulation between the tubes and the downer, the flow is very complex, very difficult to control the flow and distribution, a large change in catalytic activity.

[0009] 本领域所公知的,低碳烯烃的选择性和催化剂上的积碳量密切相关,要保证高的低碳烯烃选择性,SAP0-34催化剂上需要一定数量的积碳。 [0009] This well known in the art, is closely related to the amount of carbon deposition on the catalyst selectivity and lower olefin, to ensure a high selectivity to light olefins, SAP0-34 catalyst requires a certain amount of carbon. 目前MTO工艺所采用的主要反应器为流化床,而流化床接近于全混流反应器,催化剂积炭分布很宽,不利于提高低碳烯烃的选择性。 MTO reactor main processes used for the fluidized bed closer to the complete mixing flow reactor, a wide distribution of catalyst coke, is not conducive to improve the selectivity of light olefins. MTO工艺的剂醇比很小,生焦率较低,要实现较大的、容易控制的催化剂循环量,就需要在再生区中将催化剂上的积碳量、碳含量均匀性控制在一定水平,进而达到控制反应区内催化剂上的积碳量、碳含量均匀性的目的。 MTO process is small compared alcohol agent, a lower coke rate, to achieve a large, easy to control catalyst circulation, it is necessary carbon amount in the catalyst in the regeneration zone, the carbon content of a certain level of uniformity control the amount of carbon, thus achieving control of the reaction zone of the catalyst, the carbon content uniformity purposes. 因此,控制反应区内的催化剂积碳量和碳含量均匀性于某一水平是MTO工艺中的关键技术。 Thus, control of the reaction zone and carbon catalyst coke content uniformity to a certain level is a key technology in the MTO process.

[0010] 为解决上述问题,一些研究者提出了在流化床内设置上下两个反应区、两个流化床串联、流化床和提升管、下行床串联等技术,初步揭示了控制催化剂积碳量和碳含量均匀性的方法,取得了一定的有益效果,但也同时增加MTO工艺的复杂性、控制难度增加。 [0010] To solve the above problem, some researchers have proposed two vertically disposed reaction zone in a fluidized bed, fluidized two series, fluidized bed and a riser, the downstream beds in series technology, controlling the catalyst initially revealed the method of the amount of carbon and the carbon content uniformity, achieved some beneficial effect, but it also increases the complexity of the MTO process control more difficult. 本发明提出了通过在密相流化床中设置内构件形成多个二级反应区(再生区)的方案来解决控制催化剂积碳量和碳含量均匀性的问题,进而提高低碳烯烃的选择性。 The present invention proposes to solve the problem of controlling soot quantity and carbon content of the catalyst by uniformly programs forming a plurality of second reaction zone members (regeneration zone) is in the dense phase fluidized bed is provided, thereby increasing light olefins selected sex.

发明内容 SUMMARY

[0011] 本发明所要解决的技术问题是现有技术中存在的低碳烯烃选择性不高的问题,提供一种新的提高低碳烯烃选择性的反应装置。 [0011] The present invention solves the technical problem of selectivity to light olefins present in the prior art is not high, to provide a new improved selectivity to light olefins reaction apparatus. 该反应装置用于低碳烯烃的生产中,具有催化剂积碳均匀性好、低碳烯烃收率较高、低碳烯烃生产工艺经济性较好的优点。 The reaction apparatus for producing lower olefins, a catalyst having good carbon deposition uniformity, higher yields of light olefins, olefins produce better process economics advantages.

[0012] 为解决上述问题,本发明提供一种用于甲醇和/或二甲醚制低碳烯烃的反应装置,所述反应装置包括密相流化床反应器(2)、旋风分离器(3)、汽提器(5)、提升管(7)、密相流化床再生器(10)、旋风分离器(11)、汽提器(13)和提升管(15);其中,反应器进料管线(I)与所述密相流化床反应器(2)底部相连;所述汽提器(5)的一部分在所述密相流化床反应器(2)之中,其余部分在所述密相流化床反应器(2)下方;所述提升管(7)底部与所述汽提器(5)的底部相连,所述提升管(7)的顶部与所述密相流化床再生器(10)相连;再生器进料管线(9)与所述密相流化床再生器(10)的底部相连;所述汽提器(13)的一部分在所述密相流化床再生器(10)之中,其余部分在所述密相流化床再生器(10)下方;所述提升管(15)的底部与所述汽提器(13)的底部相连,所述提升管(15)的顶部与所述密相流化床反应器(2) [0012] In order to solve the above problems, the present invention provides a methanol and / or dimethyl ether the reaction apparatus for olefins, said reaction means comprises a dense phase fluidized bed reactor (2), the cyclone ( 3), the stripper (5), the riser (7), dense-phase fluidized bed regenerator (10), cyclone (11), stripper (13) and riser (15); wherein the reaction feed line (I) connected to the dense phase fluidized bed reactor (2) at the bottom; in a portion of the stripper (5) is in the dense phase fluidized bed reactor (2), the remaining portion of the dense phase fluidized bed reactor (2) below; said riser (7) is connected to the bottom of the bottom of said stripper (5), the top of the riser (7) with the secret -phase fluidized bed regenerator (10) is connected; regenerator feed line (9) connected to the bottom of the dense phase fluidized bed regenerator (10); and a portion of the stripper (13) is in the dense -phase fluidized bed regenerator (10) being below the remainder of the regenerator dense phase fluidized bed (10); lifting the bottom of the tube bottom (15) and said stripper (13) is connected , said riser (15) and the top of the dense phase fluidized bed reactor (2) 连,其特征在于,所述密相流化床反应器(2)和/或密相流化床再生器(10)中具有物料流动控制器(17),所述密相流化床反应器(2)由所述物料流动控制器(17)分隔为η个二级反应区,并且第I个至第η个二级反应区依序相连;所述密相流化床再生器(10)由所述物料流动控制器(17)分隔为m个二级再生区,并且第I个至第m个二级再生区依序相连;并且其中η彡2,m彡2。 Even, wherein said dense phase fluidized bed reactor (2) and / or a dense-phase fluidized bed regenerator (10) having a material flow controller (17), the dense phase fluidized bed reactor (2) by the material flow controller (17) divided into a second reaction zone η, and η through I-th secondary reaction zone sequentially connected; dense-phase fluidized bed of the regenerator (10) (17) separated by the mass flow controller is a secondary regeneration zone m, and the I-th to m-th two regeneration zone sequentially connected; and wherein η San 2, San m 2.

[0013] 在一个优选实施方案中,所述提升管(15)顶部与第I个二级反应区相连,第η个二级反应区与所述汽提器(5)上部的物料溢流口(18)相连;所述密相流化床反应器(2)的上部设有旋风分离器(3),所述旋风分离器(3)的顶部出口与产品物料管线(4)相连,所述旋风分离器(3)的底部与第η个二级反应区相连。 [0013] In a preferred embodiment, the riser (15) is connected to the top of the two I-th reaction zone, a second reaction zone of η of the stripper (5) of the upper material overflow port (18) is connected; upper part of the dense phase fluidized bed reactor (2) is provided (4) is connected to the cyclone (3), said cyclone (3) and a top outlet line material products, the bottom of the cyclone (3) and the secondary reaction zone of η connected.

[0014] 在一个优选实施方案中,所述提升管(7)的顶部与第I个二级再生区相连,第m个二级再生区与所述汽提器(13)上部的物料溢流口(18)相连;所述密相流化床再生器(10)的上部设有旋风分离器(11),所述旋风分离器(11)的顶部出口与废气管线(12)相连,所述旋风分离器(11)的底部与第m个二级再生区相连。 Top [0014] In a preferred embodiment, the riser (7) and the I-th two regeneration zone is connected to the m-th two regeneration zone and said stripper (13) of the upper material overflowing port (18) is connected; upper portion of the dense fluidized bed regenerator (10) is provided with a cyclone (11), the cyclone (11) of the top outlet of the exhaust gas line (12), said bottom of the cyclone (11) is connected to the m-th two regeneration zone.

[0015] 在一个优选实施方案中,8彡η彡3。 [0015] In a preferred embodiment, η 8 San San 3.

[0016] 在一个优选实施方案中,8彡m彡3。 [0016] In a preferred embodiment, 8 San San 3 m.

[0017] 在一个优选实施方案中,所述物料流动控制器(17)由隔板(19)、孔口(20)、物料下行流动管(21)、底部挡板(22)和取热部件(23)组成;所述孔口(20)位于所述隔板(19)的下方并与所述物料下行流动管(21)底部相连,所述底部挡板(22)位于所述物料下行流动管(21)和所述孔口(20)的底部,所述取热部件(23)固定在所述隔板(19)上。 [0017] In a preferred embodiment, the mass flow controller (17) by a partition (19), the aperture (20), the material downstream flow tube (21), a bottom flap (22) and the heat extraction member (23) the composition; the aperture (20) located below the partition plate (19) and is connected to the downstream flow tube material (21) a bottom, said bottom flap (22) positioned downstream of the material flow bottom of the tube (21) and said orifice (20), said heat extraction member (23) fixed to the partition plate (19).

[0018] 在一个优选实施方案中,所述底部挡板(22)为多孔板或无孔板。 [0018] In a preferred embodiment, the bottom flap (22) is a porous or non-porous plate.

[0019] 与已有技术方案相比,本发明的有益效果包括但不限于以下几方面: [0019] Compared with the prior art solutions, the beneficial effects of the present invention include, but are not limited to the following aspects:

[0020] (I)密相流化床具有较高的床层密度,催化剂速度较低、磨损低。 [0020] (I) dense phase fluidized bed has a high density bed, the catalyst is low speed, low wear.

[0021] (2)物料流动控制器中的物料下行流动管中的气速小于等于催化剂的最小流化速度,催化剂处于密相堆积状态,形成了催化剂的单向密相输送流,避免了相邻二级反应区(或相邻二级再生区)之间的催化剂返混,停留时间分布窄。 Gas velocity [0021] (2) Material flow controller downstream flow tube material is less than or equal to the minimum fluidization velocity of the catalyst, the catalyst dense phase in the stacked state, a one-way flow of the catalyst dense phase conveying, to avoid phase the catalyst reaction zone between two neighboring (or adjacent two regeneration zone) back mixing, residence time distribution was narrow.

[0022] (3)物料流动控制器中的取热部件具有控制反应区温度的作用。 Heat extraction member [0022] (3) mass flow controller has the effect of controlling the temperature of the reaction zone.

[0023] (4)物料流动控制器将反应区分隔为η个二级反应区,催化剂依次通过第I 二级反应区至第η 二级反应区,停留时间分布窄,待生催化剂碳含量的均匀性大幅度提高。 [0023] (4) The mass flow controller separated into the reaction zone η secondary reaction zone, the catalyst passes through the reaction zone I, two of η to the second reaction zone, the residence time distribution is narrow, the carbon content of the spent catalyst is uniformity is greatly improved.

[0024] (5)物料流动控制器将再生区分隔为m个二级再生区,催化剂依次通过第I 二级再生区至第m 二级再生区,停留时间分布窄,再生催化剂碳含量的均匀性大幅度提高。 [0024] (5) The material flow controller regeneration zone divided into m secondary regeneration zone I, two passes through the catalyst regeneration zone of the regeneration zone to the m-th two, narrow residence time distribution, a uniform carbon content of the regenerated catalyst of a substantial increase.

[0025] (6)实现了较为精确的控制再生催化剂和待生催化剂的碳含量,并且碳含量分布较为均匀,提高了低碳烯烃的选择性,并可根据需求调控碳含量来优化丙烯/乙烯的比率。 [0025] (6) to achieve a more precise control of regenerated catalyst and spent catalyst carbon content, carbon content and more uniform distribution, improving the selectivity of light olefins, and to optimize the propylene / ethylene carbon content according to the regulation requirements The ratio.

[0026] (7)因催化剂的碳含量分布较为均匀,反应区所需的催化剂藏量降低。 [0026] (7) due to the carbon content of the catalyst is more evenly distributed, reducing the storage amount of the catalyst required for the reaction zone.

[0027] (8)多个二级反应区的结构便于实现反应器的大型化。 [0027] (8) a plurality of secondary structure of the reaction zone facilitates upsizing of the reactor.

附图说明 BRIEF DESCRIPTION

[0028] 图1为本发明所述方法的流程示意图; Process [0028] Fig 1 a schematic view of the method of the present invention;

[0029] 图2为本发明所述包含4个二级反应区的密相流化床的结构示意图,其中AA剖面图中的箭头是二级反应区间的催化剂流动方向; [0029] FIG. 2 is a structural diagram of the invention with four dense fluidized bed of the second reaction zone comprises said wherein AA is a sectional view in an arrow direction of flow of the catalyst of the second reaction zone;

[0030] 图3为本发明所述包含4个二级再生区的密相流化床的结构示意图,其中BB剖面图中的箭头是二级再生区间的催化剂流动方向; [0030] FIG. 3 is a schematic structural diagram of the invention with four two dense fluidized bed of the regeneration zone comprises, wherein BB is a sectional view in an arrow direction of flow of the catalyst regeneration zone of the two;

[0031] 图4为本发明所述汽提器的结构示意图; Structure [0031] The present invention FIG. 4 is a schematic view of the stripper;

[0032] 图5为本发明所述物料流动控制器的结构示意图。 [0032] Fig 5 a schematic view of the structure of the material flow controller of the present invention.

[0033] 附图中的附图标记说明如下: [0033] The reference numerals in the drawings are as follows:

[0034] 1-反应器进料管线;1-1第I个二级反应区进料支线;1-2第2 二级反应区进料支线;1-3第3 二级反应区进料支线;1-4第4 二级反应区进料支线;2_密相流化床反应器; [0034] 1- reactor feed line; 1-1 I-th second reaction zone feed leg; 1-2 second reaction zone a second feed leg; 1-3 3 second reaction zone feed branch ; 1-4 4 second reaction zone feed leg; 2_ dense phase fluidized bed reactor;

2-1第I 二级反应区;2-2第2 二级反应区;2-3第3 二级反应区;2_4第4 二级反应区;3-旋风分离器;4_产品物料管线;5_汽提器;6_水蒸气管线;7_提升管;8_提升气管线;9-再生器进料管线;9_1第I 二级再生区进料支线;9-2第2 二级再生区进料支线;9-3第3 二级再生区进料支线;9_4第4 二级再生区进料支线;10_密相流化床再生器;10-1第I 二级再生区;10-2第2 二级再生区;10-3第3 二级再生区;10-4第4 二级再生区;11_旋风分离器;12-废气管线;13-汽提器;14-水蒸气管线;15-提升管;16-提升气管线;17-物料流动控制器;18-物料溢流口;19_隔板;20_孔口;21_物料下行流动管;22_底部挡板;23_取热部件。 The second reaction zone I, 2-1; 2-2 second reaction zone 2; 3, 2-3 second reaction zone; 2_4 of the second reaction zone 4; 3- cyclone; 4_ material product line; 5_ stripper; 6_ steam line; 7_ riser; 8_ lift gas line; 9- regenerator feed line; 9_1 regeneration zone I, two feed leg; 9-2 second two regeneration zone feed leg; 9-3 3 two regeneration zone feed leg; 4 9_4 two regeneration zone feed leg; 10_ dense-phase fluidized bed regenerator; I, two regeneration zone 10-1; 10 -2 two second regeneration zone; 3 two regeneration zone 10-3; 10-4 4 two regeneration zone; 11_ cyclone; 12- exhaust gas line; 13- stripper; 14- vapor line; riser 15; 16- lift gas line; 17- material flow controller; material overflow outlet 18; 19_ separator; 20_ aperture; 21_ material downstream of the flow tube; a 22 a bottom flap; 23_ heat extraction member.

具体实施方式 detailed description

[0035] 为了提高含氧化合物制取低碳烯烃的工艺中的低碳烯烃选择性,本发明提供了一种甲醇和/或二甲醚制低碳烯烃的反应装置,主要包括密相流化床反应器(2),旋风分离器 [0035] In order to improve the oxygen-containing compounds producing light olefin selectivity in the lower olefins process, the present invention provides a methanol and / or dimethyl ether reactor olefins, including dense-phase fluidized bed reactor (2), the cyclone

(3),汽提器(5),提升管(7),密相流化床再生器(10),旋风分离器(11),汽提器(13)和提升管(15)。 (3), stripper (5), the riser (7), dense-phase fluidized bed regenerator (10), cyclone (11), stripper (13) and riser (15). 反应器进料管线(I)与密相流化床反应器(2)的底部相连,汽提器(5) —部分在密相流化床反应器(2)中,其余部分位于密相流化床反应器(2)的下方,水蒸气管线(6)与汽提器(5)的底部相连,提升管(7)的底部与汽提器(5)的底部相连,提升气管线(8)与提升管(7)的底部相连,提升管7的顶部与密相流化床再生器(10)相连,再生器进料管线(9)与密相流化床再生器(10)的底部相连,汽提器(13)的一部分在密相流化床再生器 The reactor is connected to the feed line (I) and dense-phase fluidized bed reactor (2) the bottom of the stripper (5) - part of the dense phase fluidized bed reactor (2), the rest is in the dense phase flow It is connected to the bottom of the fluidized bed reactor (2) below, the steam line (6) and the stripper (5) is connected to the bottom of the lift pipe (7) and the bottom of the stripper (5) to enhance the gas line (8 It is connected to bottom) and the riser (7), the top of the riser 7 is connected to dense-phase fluidized bed regenerator (10), regenerator feed line (9) and the bottom of the dense fluidized bed regenerator (10) connected to a portion of the stripper (13) in a dense fluidized bed regenerator

(10)中,其余部分位于密相流化床再生器(10)下方,水蒸气管线(14)与汽提器(13)的底部相连,提升管(15)的底部与汽提器(13)的底部相连,提升气管线(16)与提升管(15)的底部相连,提升管(15)的顶部与密相流化床反应器(2)相连。 (10), the rest is in a dense phase fluidized bed regenerator (10) is connected below the bottom of the water vapor line (14) and the stripper (13), the riser (15) and the bottom of the stripper (13 ) is connected to the bottom of gas lift line (16) connected to the bottom of the riser (15), the top of the riser (15). 2) connected to the dense phase fluidized bed reactor (. 优选地,所述反应器进料管线(I)包含η个反应区进料支线(1-1,……,1_η),所述密相流化床反应器(2)由物料流动控制器(17)分隔为η个二级反应区(2-1,……,2-η),η彡2,优选为8彡η彡3 ;η个反应区进料支线分别与η个二级反应区相连;第I个至第η个二级反应区依序相连,提升管(15)的顶部与第I个二级反应区相连,第η个二级反应区与汽提器(5)上部的物料溢流口(18)相连,密相流化床反应器(2)的上部设有旋风分离器(3),旋风分离器(3)的顶部出口与产品物料管线(4)相连,旋风分离器(3)的底部与第η个二级反应区相连。 Preferably, the reactor feed line (I) comprises reaction zone feed η branch (1-1, ......, 1_η), the dense phase fluidized bed reactor (2) by a material flow controller ( 17) is partitioned into two [eta] a reaction zone (2-1, ......, 2-η), η San 2, preferably 8 San San [eta] 3; η reaction zone feed branch respectively [eta] a second reaction zone connected; through I-th secondary reaction zone η connected sequentially, top of the riser (15) is connected to two I-th reaction zone, the secondary reaction zone η stripper (5) of the upper portion material overflow outlet (18) connected to an upper portion of the dense phase fluidized bed reactor (2) is provided (4) is connected to the cyclone (3), a cyclone (3) and a top outlet line product material, cyclones a bottom (3) and the secondary reaction zone of η connected.

[0036] 优选地,所述再生器进料管线(9)包含m个再生区进料支线(9-1,……,9_m),所述密相流化床再生器(10)由物料流动控制器(17)分隔为m个二级再生区(10-1,……,10-m),m彡2,优选为8彡m彡3 ;m个再生区进料支线分别与m个二级再生区相连;第I个至第m个二级再生区依序相连,提升管(7)的顶部与第I个二级再生区相连,第m个二级再生区与汽提器(13)上部的物料溢流口(18)相连,密相流化床再生器(10)的上部设有旋风分离器(11),旋风分离器(11)的顶部出口与废气管线(12)相连,旋风分离器(11)的底部与第m个二级再生区相连。 [0036] Preferably, said regenerator feed line (9) comprising m regeneration zone feed branch (9-1, ......, 9_m), the dense-phase fluidized bed regenerator (10) by the material flow the controller (17) divided into m secondary regeneration zone (10-1, ......, 10-m), m San 2, preferably 8 m San San. 3; m regeneration zone feed two legs respectively the m stage connected to the regeneration zone; the I-th to m-th two regeneration zone sequentially connected to top of the riser (7) is connected to the first secondary regeneration zone I, the m-th two regeneration zone and the stripper (13 ) upper material overflow outlet (18) connected to an upper portion of the dense phase fluidized bed regenerator (10) is provided connected to the cyclone (11), cyclone (11) and a top flue gas outlet line (12), bottom of the cyclone (11) is connected to the m-th two regeneration zone.

[0037] 优选地,所述物料流动控制器(17)由隔板(19)、孔口(20)、物料下行流动管(21)、底部挡板(22)和取热部件(23)组成。 [0037] Preferably, the mass flow controller (17) by a partition (19), the aperture (20), the material downstream flow tube (21), a bottom flap (22) and the heat extraction member (23) composed of . 孔口(20)位于隔板(19)的下方,与物料下行流动管(21)的底部相连,底部挡板(22)可采用多孔板或无孔板,其位于物料下行流动管(21)和孔口(20)的底部,取热部件(23)固定在隔板(19)上。 Below the aperture (20) located in the separator (19), the bottom material downstream flow tube (21) is connected to a bottom flap (22) can be non-porous or perforated plate, located downstream of material flow tube (21) and a bottom opening (20), the heat extraction member (23) fixed to the partition (19).

[0038] 在一个优选实施方案中,本发明所述的甲醇制低碳烯烃的流程示意图如图1所示。 [0038] In a preferred embodiment, the MTO process of the present invention is shown in Fig.1. 主要为甲醇和/或二甲醚的原料进入密相流化床反应器(2),与催化剂接触,生成气相产品物流和待生催化剂,气相产品物流和夹带的待生催化剂进入旋风分离器(3),气相产品物流经旋风分离器的出口进入后续分离工段,夹带的待生催化剂经旋风分离器的料腿进入第η个二级反应区,再生催化剂经过汽提器(13)、提升管(15)进入密相流化床反应器2,并依序经过第I个至第η个二级反应区,积碳后形成待生催化剂,待生催化剂再经过汽提器(5)、提升管(7)进入密相流化床再生器(10),并依序经过第I个至第m个二级再生区,烧炭后形成再生催化剂。 Into the main dense phase fluidized bed reactor (2) methanol and / or dimethyl ether raw materials, contact with the catalyst to produce the product gas stream and spent catalyst, the product gas stream and entrained spent catalyst into the cyclone ( 3), the product gas stream through the outlet into the subsequent separation cyclone stage, entrained spent catalyst through a cyclone dipleg into the secondary reaction zone of η, the regenerated catalyst through the stripper (13), the riser (15) enters the dense-phase fluidized bed reactor 2, and sequentially passes through the I-th η secondary reaction zone, the spent catalyst is formed after carbon deposition, and then through the spent catalyst stripper (5) to enhance the tube (7) into the dense-phase fluidized bed regenerator (10), and sequentially pass through the I-th to m-th two regeneration zone, the regenerated catalyst is formed charcoal. 所述催化剂优选包括SAPO分子筛的催化剂,进一步优选为包括SAP0-34分子筛的催化剂。 The catalyst preferably comprises a SAPO molecular sieve catalyst, more preferably a molecular sieve catalyst comprising SAP0-34.

[0039] 在一个具体实施方案中,本发明的包含4个二级反应区的密相流化床的结构示意图如图2所示,AA剖面图中的箭头是二级反应区间的催化剂流动方向。 [0039] In one particular embodiment, the present invention comprises a dense phase fluidized bed in the reaction zone structure 4 two schematic diagram shown in Figure 2, AA is a sectional view in the direction of flow arrow catalyst two reaction sections . 3个物料流动控制器(17)和一个挡板竖直设置,将密相流化床反应区分隔为4个二级反应区,催化剂依序通过第I个至第4个二级反应区,然后进入汽提器。 3 material flow controller (17) and a baffle disposed vertically, the dense fluidized bed reaction zone is divided into four second reaction zone, the catalyst sequentially through the I-th through fourth secondary reaction zone, then into the stripper.

[0040] 在一个具体实施方案中,本发明的包含4个二级再生区的密相流化床的结构示意图如图3所示,BB剖面图中的箭头是二级再生区间的催化剂流动方向。 [0040] In one particular embodiment, the present invention comprises a dense phase fluidized bed of the regeneration zone structure 4 two schematic diagram shown in Figure 3, BB is a sectional view in a flow direction of an arrow a catalyst regeneration section two . 3个物料流动控制器(17)和一个挡板竖直设置,将密相流化床再生区分隔为4个二级再生区,催化剂依序通过第I个至第4个二级再生区,然后进入汽提器。 3 material flow controller (17) and a baffle disposed vertically, the dense fluidized bed regeneration zone divided into two regeneration zone 4, the catalyst sequentially through the I-th through fourth secondary regeneration zone, then into the stripper.

[0041] 优选地,本发明所述的汽提器(5和13)的结构示意图如图4所示。 [0041] Preferably, the structure of the stripper (5 and 13) of the present invention is schematically shown in Fig. 汽提器(5)上部管壁上的开口作为第η个二级反应区与汽提器(5)之间的物料溢流口(18);汽提器(13)上部管壁上的开口作为第m个二级再生区与汽提器(13)之间的物料溢流口(18)。 Opening an upper wall stripper (5) as a first overflow outlet η materials (18) between the secondary reaction zone and the stripper (5); an opening on an upper wall (13) stripper as an overflow of material between the two m-th reproduced region and the stripper (13) (18).

[0042] 优选地,本发明所述的物料流动控制器的结构示意图如图5所示。 [0042] Preferably, the structural material flow controller according to the present invention is schematically shown in Fig. 物料流动控制器(17)由隔板(19)、孔口(20)、物料下行流动管(21)、底部挡板(22)和取热部件(23)组成。 Material flow controller (17) by a partition (19), the aperture (20), the material downstream flow tube (21), a bottom flap (22) and the heat extraction member (23) components. 催化剂由下行流动管上方进入物料下行流动管,其中气体表观线速度小于等于最小流化速度,物料下行流动管内的催化剂处于密相堆积状态,形成物料流动推动力,推动催化剂经过孔口流入其后的二级反应区(或再生区)。 Above the catalyst enters the downlink flow tube downstream of the flow tube material, wherein a gas superficial linear velocity is less than equal to the minimum fluidization velocity of the catalyst in the down flow tube material deposited in dense phase state, a material flow push in which the catalyst flows through the orifice after the secondary reaction zone (or the regeneration zone). 取热部件可采用盘管结构,固定于隔板之上。 Heat removal coil structure member can be fixed to the top of the separator.

[0043] 优选地,所述密相流化床反应区内气体表观线速度为0.1-1.5m/s ;所述密相流化床再生区内气体表观线速度为0.1-1.5m/s ;所述物料流动控制器内气体表观线速度小于等于催化剂的最小流化速度;所述催化剂优选包括SAPO分子筛的催化剂,进一步优选为包括SAP0-34分子筛的催化剂;所述反应区底部设有进料口,进料包括甲醇和/或二甲醚等;所述汽提器(13)的汽提介质包含水蒸气;所述再生区(10)底部设有再生介质入口,再生介质包括空气、贫氧空气、水蒸气等;所述反应区(2)的反应温度为400-550°C,床层密度为200-1200kg/m3,催化剂平均积炭量由第I个二级反应区至第η个二级反应区依次递增,第I个二级反应区的平均积炭量为0.5-3wt%,第η个二级反应区的平均积炭量为7-10wt% ;所述再生区(10)的反应温度为500-700°C,床层密度为200-1200kg/m3,催化剂平均积炭量由第I个二 [0043] Preferably, the dense phase fluidized bed reaction zone gas superficial linear velocity of 0.1-1.5m / s; the regeneration zone dense phase fluidized bed gas superficial linear velocity of 0.1-1.5m / S; gas superficial linear velocity of the material flow controller is less than the minimum fluidization velocity equal to the catalyst; said catalyst preferably comprises a SAPO molecular sieve catalyst, more preferably the catalyst comprising a molecular sieve SAP0-34; located at the bottom of the reaction zone feed inlet, a feed comprising methanol and / or dimethyl ether and the like; the stripper (13) of the stripping medium comprises steam; the regeneration zone (10) is provided with a bottom inlet regeneration medium, regeneration medium comprising air, oxygen-depleted air, water vapor and the like; the reaction temperature of the reaction zone (2) is 400-550 ° C, the bed density 200-1200kg / m3, the average amount of coke from the catalyst secondary reaction zone I, η to the second secondary reaction zone in ascending order, the average amount of coke I, secondary reaction zone 0.5-3wt%, of the average amount of coke η secondary reaction zone is 7-10wt%; the regeneration the reaction temperature zone (10) is 500-700 ° C, the bed density 200-1200kg / m3, the average amount of coke from the catalyst I-th two 再生区至第m个二级再生区依次递减,第I个二级再生区的平均积炭量为 The regeneration zone to the m-th two regeneration zone in descending order, of the average amount of coke secondary regeneration zone I is

3-10wt%,第m个二级再生区的平均积炭量为0-3wt%。 3-10wt%, of the average amount of coke m secondary regeneration zone is 0-3wt%. 采用本发明的方法,可以达到控制催化剂积碳量、改善碳含量均匀性以及提高低碳烯烃选择性的目的,具有较大的技术优势,可用于低碳烯烃的工业生产中。 Using the method of the invention, the catalyst can be to control the amount of carbon, the carbon and to improve content uniformity purpose of improving selectivity to light olefins, with great technical advantages, it can be used for industrial production of lower olefins.

[0044] 为更好地说明本发明,便于理解本发明的技术方案,本发明的典型但非限制性的实施例如下: [0044] To better illustrate the present invention, to facilitate understanding of the technical solutions of the present invention, the present invention is exemplary but non-limiting embodiment are as follows:

[0045] 实施例1 [0045] Example 1

[0046] 密相流化床反应器内设置4个二级反应区,密相流化床再生器内设置4个二级再生区,主要为甲醇和/或二甲醚的原料进入密相流化床反应器,与包括SAP0-34分子筛的催化剂接触,生成的气相产品物流和待生催化剂,气相物料和夹带的待生催化剂进入旋风分离器,气相产品物流经旋风分离器的出口进入后续分离工段,夹带的待生催化剂经旋风分离器的料腿进入第4个二级反应区。 [0046] The second reaction zone 4 is provided within the dense phase fluidized bed reactor, provided with four two regeneration zone dense phase fluidized bed regenerator, mainly methanol and / or dimethyl ether feedstock enters dense phase flow bed reactor, with the catalyst comprising a molecular sieve SAP0-34 resulting vapor product stream and spent catalyst, the material gas and entrained spent catalyst into the cyclone, the product gas stream through the outlet into the subsequent separation cyclone stage, entrained spent catalyst through a cyclone dipleg into the fourth reaction zone two. 再生催化剂经过汽提器、提升管进入密相流化床反应器,并依序经过第I个至4个二级反应区,积碳后形成待生催化剂,待生催化剂再经过汽提器、提升管进入密相流化床再生器,并依序经过第I个至4个二级再生区,烧炭后形成再生催化剂。 Regenerated catalyst through the stripper, into the dense phase fluidized bed riser reactor, and sequentially passes through the first two to four I reaction zone, the spent catalyst is formed after carbon deposition, and then through the spent catalyst stripper, dense fluidized bed into the riser regenerator, and sequentially passes through the first two to four I regeneration zone, the regenerated catalyst is formed charcoal. 密相流化床反应器反应条件为:反应温度为400°C,气相线速度为0.3m/s,床层密度为1000kg/m3,第I个二级反应区的平均积炭量为2wt%,第2个二级反应区的平均积炭量为6wt%,第3个二级反应区的平均积炭量为8wt%,第4个二级反应区的平均积炭量为1wt % ;密相流化床再生器反应条件为:反应温度为500°C,气相线速度为0.3m/s,床层密度为1000kg/m3,第I个二级再生区的平均积炭量为7wt%,第2个二级再生区的平均积炭量为4wt%,第3个二级再生区的平均积炭量为2wt%,第4个二级再生区的平均积炭量为lwt%。 The reaction conditions for the dense phase fluidized bed reactor as follows: reaction temperature of 400 ° C, vapor linear velocity of 0.3m / s, the bed density 1000kg / m3, the average amount of coke I-th second reaction zone is 2wt% the average amount of coke second secondary reaction zone 6wt%, the average amount of coke third secondary reaction zone 8wt%, the average amount of coke on the second reaction zone 4 is 1wt%; density fluidized bed regenerator reaction conditions are: a reaction temperature of 500 ° C, vapor linear velocity of 0.3m / s, the bed density 1000kg / m3, the average amount of coke I, secondary regeneration zone is 7wt%, the average amount of the second secondary coke regeneration zone to 4wt%, the average amount of coke third secondary regeneration zone to 2wt%, of the average amount of coke in the regeneration zone 4 is two lwt%. 反应产品采用在线气相色谱分析,低碳烯烃碳基收率为91.lwt%。 The reaction products using online gas chromatography analysis, a yield of the carbon-based olefins 91.lwt%.

[0047] 实施例2 [0047] Example 2

[0048] 密相流化床反应器内设置3个二级反应区,密相流化床再生器内设置2个二级再生区,主要为甲醇和/或二甲醚的原料进入密相流化床反应器,与包括SAP0-34分子筛的催化剂接触,生成的气相产品物流和待生催化剂,气相物料和夹带的待生催化剂进入旋风分离器,气相产品物流经旋风分离器的出口进入后续分离工段,夹带的待生催化剂经旋风分离器的料腿进入第3 二级反应区。 [0048] 3 is provided within the second reaction zone dense phase fluidized bed reactor, provided two two regeneration zone dense phase fluidized bed regenerator, mainly methanol and / or dimethyl ether feedstock enters dense phase flow bed reactor, with the catalyst comprising a molecular sieve SAP0-34 resulting vapor product stream and spent catalyst, the material gas and entrained spent catalyst into the cyclone, the product gas stream through the outlet into the subsequent separation cyclone stage, entrained spent catalyst through the dipleg of the cyclone 3 into the second reaction zone. 再生催化剂经过汽提器、提升管进入密相流化床反应器,并依序经过第I个至3个二级反应区,积碳后形成待生催化剂,待生催化剂再经过汽提器、提升管进入密相流化床再生器,并依序经过第I个至2个二级再生区,烧炭后形成再生催化剂。 Regenerated catalyst through the stripper, into the dense phase fluidized bed riser reactor, and sequentially passes through the first two to three I-th reaction zone, the spent catalyst is formed after carbon deposition, and then through the spent catalyst stripper, dense fluidized bed into the riser regenerator, and sequentially pass through the I-th to 2 secondary regeneration zone, the regenerated catalyst is formed charcoal. 密相流化床反应器反应条件为:反应温度为450°C,气相线速度为0.5m/s,床层密度为900kg/m3,第I个二级反应区的平均积炭量为3wt%,第2个二级反应区的平均积炭量为7wt%,第3 二级反应区的平均积炭量为9wt% ;密相流化床再生器反应条件为:反应温度为600°C,气相线速度为0.7m/s,床层密度为700kg/m3,第I个二级再生区的平均积炭量为4wt%,第2个二级再生区的平均积炭量为2wt%。 The reaction conditions for the dense phase fluidized bed reactor: the reaction temperature was 450 ° C, vapor linear velocity of 0.5m / s, the bed density of 900kg / m3, the average amount of coke I-th second reaction zone is 3wt% the average amount of coke second secondary reaction zone 7wt%, the average amount of coke on the second reaction zone 3 is 9wt%; dense-phase fluidized bed reactor regenerator conditions: reaction temperature of 600 ° C, gas linear velocity of 0.7m / s, the bed density of 700kg / m3, the average amount of coke I, secondary regeneration zone of 4wt%, the average amount of the second secondary coke regeneration zone to 2wt%. 反应产品采用在线气相色谱分析,低碳烯烃碳基收率为90.5wt%。 The reaction products using online gas chromatography analysis, a yield of the carbon-based olefins 90.5wt%.

[0049] 实施例3 [0049] Example 3

[0050] 密相流化床反应器内设置6个二级反应区,密相流化床再生器内设置5个二级再生区,主要为甲醇和/或二甲醚的原料进入密相流化床反应器,与包括SAP0-34分子筛的催化剂接触,生成的气相产品物流和待生催化剂,气相物料和夹带的待生催化剂进入旋风分离器,气相产品物流经旋风分离器的出口进入后续分离工段,夹带的待生催化剂经旋风分离器的料腿进入第6个二级反应区。 [0050] The second reaction zone 6 is provided within a dense phase fluidized bed reactor, disposed within the 5 second regeneration zone dense phase fluidized bed regenerator, mainly methanol and / or dimethyl ether feedstock enters dense phase flow bed reactor, with the catalyst comprising a molecular sieve SAP0-34 resulting vapor product stream and spent catalyst, the material gas and entrained spent catalyst into the cyclone, the product gas stream through the outlet into the subsequent separation cyclone stage, entrained spent catalyst through the dipleg of the cyclone 6 into the first two reaction zones. 再生催化剂经过汽提器、提升管进入密相流化床反应器,并依序经过第I至6个二级反应区,积碳后形成待生催化剂,待生催化剂再经过汽提器、提升管进入密相流化床再生器,并依序经过第I至5个二级再生区,烧炭后形成再生催化剂。 Regenerated catalyst through the stripper, into the dense phase fluidized bed riser reactor, and sequentially passes through the first two I to 6, a reaction zone, the soot formation in the spent catalyst, spent catalyst and then through the stripper, lift tube into the dense fluidized bed regenerator, and 5 to sequentially pass through the first two I regeneration zone, the regenerated catalyst is formed charcoal. 密相流化床反应器反应条件为:反应温度为480°C,气相线速度为0.7m/s,床层密度为700kg/m3,第I个二级反应区的平均积炭量为lwt%,第2个二级反应区的平均积炭量为3wt%,第3个二级反应区的平均积炭量为4wt%,第4个二级反应区的平均积炭量为5wt%,第5个二级反应区的平均积炭量为6wt%,第6个二级反应区的平均积炭量为7wt% ;密相流化床再生器反应条件为:反应温度为650°C,气相线速度为l.0m/s,床层密度为500kg/m3,第I个二级再生区的平均积炭量为5wt%,第2个二级再生区的平均积炭量为3wt%,第3个二级再生区的平均积炭量为2wt%,第4个二级再生区的平均积炭量为lwt%,第5个二级再生区的平均积炭量为0.01wt%。 The reaction conditions for the dense phase fluidized bed reactor as follows: reaction temperature of 480 ° C, vapor linear velocity of 0.7m / s, the bed density of 700kg / m3, the average amount of coke I-th second reaction zone is lwt% the average amount of coke second secondary reaction zone 3wt%, the average amount of coke third secondary reaction zone 4wt%, the average amount of coke on the second reaction zone 4 is 5wt%, of the average amount of coke 5 second reaction zone 6wt%, of the average amount of coke second reaction zone 6 is 7wt%; dense-phase fluidized bed reactor regenerator conditions: reaction temperature of 650 ° C, vapor phase the line speed was l.0m / s, the bed density of 500kg / m3, the average amount of coke I, secondary regeneration zone is 5wt%, the average amount of the second secondary coke regeneration zone to 3wt%, of the average amount of coke three second regeneration zone is 2wt%, of the average amount of coke in the regeneration zone 4 is two lwt%, the average amount of coke of 5 second regeneration zone to 0.01wt%. 反应产品采用在线气相色谱分析,低碳烯烃碳基收率为91.4wt%。 The reaction products using online gas chromatography analysis, a yield of the carbon-based olefins 91.4wt%.

[0051] 以上已对本发明进行了详细描述,但本发明并不局限于本文所描述具体实施方式。 [0051] The present invention has above been described in detail, but the present invention is not limited to the specific embodiments described herein. 本领域技术人员理解,在不背离本发明范围的情况下,可以作出其他更改和变形。 Those skilled in the art understand, without departing from the scope of the present invention, other changes and variations may be made. 本发明的范围由所附权利要求限定。 Scope of the invention defined by the appended claims.

Claims (7)

  1. 1.一种用于甲醇和/或二甲醚制低碳烯烃的反应装置,其特征在于,所述反应装置包括密相流化床反应器(2)、旋风分离器(3)、汽提器(5)、提升管(7)、密相流化床再生器(10)、旋风分离器(11)、汽提器(13)和提升管(15);其中,反应器进料管线(I)与所述密相流化床反应器(2)底部相连;所述汽提器(5)的一部分在所述密相流化床反应器(2)之中,其余部分在所述密相流化床反应器(2)下方;所述提升管(7)底部与所述汽提器(5)的底部相连,所述提升管(7)的顶部与所述密相流化床再生器(10)相连;再生器进料管线(9)与所述密相流化床再生器(10)的底部相连;所述汽提器(13)的一部分在所述密相流化床再生器(10)之中,其余部分在所述密相流化床再生器(10)下方;所述提升管(15)的底部与所述汽提器(13)的底部相连,所述提升管(15)的顶部与所述密相流化床反应器(2)相连,其中所述密相 A methanol and / or dimethyl ether the reaction apparatus for light olefins, characterized in that the reaction means comprises a dense phase fluidized bed reactor (2), the cyclone (3), stripped (5), the riser (7), dense-phase fluidized bed regenerator (10), cyclone (11), stripper (13) and riser (15); wherein the reactor feed line ( I) with the dense phase fluidized bed reactor (2) connected to the base; a portion of the stripper (5) is in the dense phase fluidized bed reactor 2) into the (rest of the secret phase fluidized bed reactor (2) below; said riser (7) is connected to the bottom of the bottom of said stripper (5), the top of the riser (7) and said dense phase fluidized bed regenerator (10) is connected; regenerator feed line (9) connected to the bottom of the dense phase fluidized bed regenerator (10); and a portion of the stripper (13) is regenerated in the dense phase fluidized bed (10) in the rest (10) below the said dense fluidized bed regenerator; lift the bottom of the tube is connected to a bottom (15) and said stripper (13), said riser top (15) (2) connected to the dense phase fluidized bed reactor, wherein the dense phase 流化床反应器(2)和/或密相流化床再生器(10)中具有物料流动控制器(17),所述密相流化床反应器(2)由所述物料流动控制器(17)分隔为η个二级反应区,并且第I个至第η个二级反应区依序相连;所述密相流化床再生器(10)由所述物料流动控制器(17)分隔为m个二级再生区,并且第I个至第m个二级再生区依序相连;并且其中η > 2, m > 2。 The fluidized bed reactor (2) and / or a dense-phase fluidized bed regenerator (10) having a material flow controller (17), the dense phase fluidized bed reactor (2) by the material flow controller (17) divided into a second reaction zone η, and η through I-th secondary reaction zone sequentially connected; dense-phase fluidized bed of the regenerator (10) by the material flow controller (17) m partitioned into secondary regeneration zone, and the I-th to m-th two regeneration zone sequentially connected; and wherein η> 2, m> 2.
  2. 2.根据权利要求1所述的反应装置,其特征在于,所述提升管(15)顶部与第I个二级反应区相连,第η个二级反应区与所述汽提器(5)上部的物料溢流口(18)相连;所述密相流化床反应器(2)的上部设有旋风分离器(3),所述旋风分离器(3)的顶部出口与产品物料管线(4)相连,所述旋风分离器(3)的底部与第η个二级反应区相连。 2. A reaction apparatus according to claim 1, wherein said riser (15) is connected to the top of the two I-th reaction zone, a second reaction zone of η of the stripper (5) an upper material overflow outlet (18) is connected; upper part of the dense phase fluidized bed reactor (2) is provided with a cyclone (3), said cyclone (3) of the top outlet line and the product material ( 4) connected to the bottom of the cyclone (3) and the secondary reaction zone of η connected.
  3. 3.根据权利要求1所述的反应装置,其特征在于,所述提升管(7)的顶部与第I个二级再生区相连,第m个二级再生区与所述汽提器(13)上部的物料溢流口(18)相连;所述密相流化床再生器(10)的上部设有旋风分离器(11),所述旋风分离器(11)的顶部出口与废气管线(12)相连,所述旋风分离器(11)的底部与第m个二级再生区相连。 3. The reaction apparatus according to claim 1, characterized in that the top of the riser (7) is connected to the first secondary regeneration zone I, the m-th two regeneration zone and said stripper (13 ) upper material overflow outlet (18) is connected; upper portion of the dense fluidized bed regenerator (10) is provided with a cyclone (11), the cyclone (11) and the exhaust gas outlet of the top line ( 12) connected to the bottom of the cyclone (11) to the first regeneration zone is connected to the m-th two.
  4. 4.根据权利要求1所述的反应装置,其特征在于,8 > η > 3。 4. The reaction apparatus according to claim 1, characterized in that, 8> η> 3.
  5. 5.根据权利要求1所述的反应装置,其特征在于,8 > m > 3。 The reaction apparatus according to claim 1, characterized in that, 8> m> 3.
  6. 6.根据权利要求1-5任一项所述的反应装置,其特征在于,所述物料流动控制器(17)由隔板(19)、孔口(20)、物料下行流动管(21)、底部挡板(22)和取热部件(23)组成;所述孔口(20)位于所述隔板(19)的下方并与所述物料下行流动管(21)底部相连,所述底部挡板(22)位于所述物料下行流动管(21)和所述孔口(20)的底部,所述取热部件(23)固定在所述隔板(19)上。 6. The reaction apparatus according to any one of claims 1-5, characterized in that said material flow controller (17) by a partition (19), the aperture (20), the material downstream flow tube (21) , the bottom flap (22) and the heat extraction member (23) consisting of; the aperture (20) in said partition plate (19) and below the material downstream flow tube (21) connected to a bottom portion baffle (22) located at the bottom of the down flow tube material (21) and said orifice (20), said heat extraction member (23) fixed to the partition plate (19).
  7. 7.根据权利要求6所述的反应装置,其特征在于,所述底部挡板(22)为多孔板或无孔板。 7. The reaction apparatus according to claim 6, characterized in that the bottom flap (22) is a porous or non-porous plate.
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