Búsqueda Imágenes Maps Play YouTube Noticias Gmail Drive Más »
Iniciar sesión
Usuarios de lectores de pantalla: deben hacer clic en este enlace para utilizar el modo de accesibilidad. Este modo tiene las mismas funciones esenciales pero funciona mejor con el lector.

Patentes

  1. Búsqueda avanzada de patentes
Número de publicaciónCN104672045 A
Tipo de publicaciónSolicitud
Número de solicitudCN 201310648651
Fecha de publicación3 Jun 2015
Fecha de presentación3 Dic 2013
Fecha de prioridad3 Dic 2013
También publicado comoCN104672045B
Número de publicación201310648651.7, CN 104672045 A, CN 104672045A, CN 201310648651, CN-A-104672045, CN104672045 A, CN104672045A, CN201310648651, CN201310648651.7
Inventores张涛, 叶茂, 刘中民
Solicitante中国科学院大连化学物理研究所
Exportar citaBiBTeX, EndNote, RefMan
Enlaces externos:  SIPO, Espacenet
Reaction device for preparing low-carbon olefin by employing methyl alcohol and/or dimethyl ether
CN 104672045 A
Resumen
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.
Reclamaciones(7)  traducido del chino
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。 A methanol and / or dimethyl ether reactor system for light olefins, wherein the reaction unit comprises a dense phase fluidized bed reactor (2), cyclone (3), stripping (5), riser (7), dense-phase fluidized bed regenerator (10), the cyclone (11), stripper (13) and the riser (15); wherein the reactor feed line ( I) and the dense phase fluidized bed reactor (2) connected to the bottom; portion of the stripper (5) in the dense phase fluidized bed reactor (2) respectively, the rest of the secret phase fluidized bed reactor (2) below; said riser (7) connected to said stripper (5) of the bottom of the bottom, said riser (7) on top of the dense phase fluidized bed regenerator (10) is connected; regenerator feed line (9) is connected to the bottom of the dense phase fluidized bed regenerator (10); a portion of the stripper (13) in said dense phase fluidized bed regenerator (10) among the rest of the dense phase fluidized bed in the regenerator (10) below; said lifting connected to the stripper (13) in the bottom of the tube (15) in the bottom of the riser top (15) and said dense phase fluidized bed reactor (2) is connected, wherein the dense phase fluidized bed reactor (2) and / or dense phase fluidized bed regenerator (10) having a material flow The controller (17), said dense phase fluidized bed reactor (2) by the material flow controller (17) is divided into η secondary reaction zone, and the first I th to η according to a second reaction zone Sequence connected; said dense phase fluidized bed regenerator (10) of material by said fluid controller (17) is divided into m secondary regeneration zone, and the I-th to m-th secondary regeneration zone sequentially connected; and wherein η> 2, m> 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. The reaction apparatus according to claim 1, wherein said riser (15) is connected to the top of the I-th second reaction zone, a second reaction zone the first η with the stripper (5) the upper material overflow outlet (18) is connected; upper part of the dense phase fluidized bed reactor (2) is provided with a cyclone (3), the cyclone (3) of the top export pipeline materials and products ( 4) is connected to the bottom of the cyclone (3) and a second reaction zone the first η connected.
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 said riser (7) is connected to the top of the first secondary regeneration zone I, the m-th secondary regeneration zone and the stripper (13 ) upper part of the overflow gate material (18) is connected; upper part of the dense phase fluidized bed regenerator (10) is provided with a cyclone (11), the cyclone (11) of the top outlet and an exhaust line ( 12) is connected to the bottom of the cyclone (11) is connected to the m-th secondary regeneration zone.
4.根据权利要求1所述的反应装置,其特征在于,8 > η > 3。 The reaction apparatus according to claim 1, characterized in that, 8> η> 3.
5.根据权利要求1所述的反应装置,其特征在于,8 > m > 3。 5. The reaction apparatus according to claim 1, characterized in that, 8> m> 3.
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 according to any one of claims 1-5, characterized in that the material flow controller (17) by a partition plate (19), the orifice (20), the material downstream flow tube (21) , the bottom of the baffle (22) and the heat removal means (23) consisting of; below the aperture (20) in said partition plate (19) and with said material downstream flow tube (21) is connected to the bottom, the bottom baffle (22) located downstream of the material flow tube bottom (21) and said orifice (20), said heat extraction member (23) fixed to said partition plate (19).
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 of the bezel (22) is a porous or non-porous plate.
Descripción  traducido del chino
—种用于甲醇和/或二甲醚制低碳烯烃的反应装置 - Kind of reactor, methanol and / or dimethyl ether to olefins used

技术领域 TECHNICAL 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 reactor for production of light 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] olefins, namely 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 route, but due to the limited supply of oil resources and higher prices, the cost of oil resources by the production of ethylene, propylene increasing. 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. 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。 Conversion of methanol to olefins (MTO) process are more and more attention has been realized 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, olefins, particularly propylene, increasing demand, analysis of Intermec (CMAI) analysis said that in 2016, ethylene demand will average 4.3% growth rate, the demand for propylene will be with an 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 the rapid growth of China's economy, China's demand for ethylene and propylene annual growth rate in excess of 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] the early 1980s, UCC has successfully developed a series of molecular sieves SAPO, which SAP0-34 molecular sieve catalyst when used in MTO reaction exhibit excellent catalytic performance, with high selectivity to light olefins, and active high, but the catalyst in use for some time and loss of activity due to the coke. 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 molecular sieve catalyst obvious induction period during use, in the induction period, the selectivity of lower olefins, paraffins high selectivity with increasing reaction time, low-carbon olefin selectivity increased gradually induce After the period, the catalyst within a certain time maintaining high selectivity and high activity, with the continued extension of time, the catalyst activity declined 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 fast fluidized bed reactor, the gas velocity in the gas phase after the dense phase reaction zone lower the reaction was completed, the rapid rise to the inner diameter becomes smaller After a quick partition, using a special gas-solid separation equipment initially separated 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 and catalyst rapid separation, effectively preventing 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 the conventional bubbling fluidized bed reactor, the fast fluidized bed reactor volume required to hiding diameter and catalyst 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。 But this method of carbon-based light olefins yields are generally about 77%, there is a lower yield of light olefins problem.

[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 for improving the yield of light olefins, which uses methanol to light olefins in a first reaction zone an upper portion provided with a second reaction zone and the second reaction zone is greater than the first diameter The reaction zone to the first reaction zone to increase product gas at the outlet of the second reaction zone residence time, so that the unreacted methanol, dimethyl ether and carbon produced hydrocarbon reaction was continued for four or more, to improve the yield of light olefins purpose, although the method can improve the yield of light olefins to some extent, but since the first reaction zone with a catalyst has more carbon, and four or more carbon hydrocarbon pyrolysis requires high catalyst activity, This method of carbon second reaction zone a hydrocarbon conversion efficiency of more than four still low, thus resulting in low yields of light olefins.

[0006] CN102276406A公布了一种增产丙烯的生产方法。 [0006] CN102276406A announced an increase propylene production methods. 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。 The technology set three reaction zones, a first reaction zone for rapid bed conversion of methanol to olefins, the riser reaction zone and the second reaction zone in series rapid 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。 This patent carbon four or more hydrocarbons and other substances in the riser reaction zone and the second reaction zone fast bed the residence time is short, the conversion efficiency is low, 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 announced an internal arrangement of a fluidized bed reactor riser reactor and used to improve 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。 The first material into the fluidized bed reaction zone, in contact with the catalyst to produce light olefins including product, while forming the spent catalyst; spent catalyst into the regenerator portion of the regeneration, the formation of regenerated catalyst, into the outlet end portion located inside the reaction zone riser, contact with the second material, the spent catalyst to enhance the reaction zone; regenerated catalyst fluidized bed reactor reaction zone returned. 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。 Reaction apparatus disclosed in this patent no stripping section, the spent catalyst will carry part of the product gas into the regenerator, combustion with oxygen, to reduce production 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 released methanol to olefins technology to set a fast bed, downer and riser reaction zone three. 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, rapid bed, improve circulation between the tube and the downer, the flow is very complicated, very difficult to control the flow distribution and a larger 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] known in the art, the amount of coke selectivity and catalyst on the light olefins are closely related, to ensure that the high selectivity of light olefins, SAP0-34 catalysts require 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。 At present the main reactor MTO process used for the fluidized bed, and the fluidized bed near CSTR catalyst coke distribution is very broad, 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。 Agent alcohol MTO process than small, low coke rate, to achieve greater circulation amount of the catalyst is easy to control, you need the amount of coke on the catalyst in the regeneration zone, the carbon content uniformity control at a certain level the amount of carbon, and thus to control the reaction zone on 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。 Therefore, control of the reaction zone catalyst coke and carbon content is a certain level of uniformity in the MTO process in key technologies.

[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 setting upper and lower reaction zone in a fluidized bed, two fluidized bed series, fluidized bed and riser, downer tandem technology, initially revealed control catalyst the amount of carbon and a carbon content uniformity, achieved some beneficial effects, 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 adoption of the program in the dense phase fluidized bed set member forming a plurality of second reaction zone (the regeneration zone) to solve the control catalyst coke and carbon content uniformity issues, thereby increasing choice of light olefins sex.

发明内容 SUMMARY OF THE INVENTION

[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。 Technical Problem [0011] The present invention solves the olefins present in the prior art selectivity is not high, to provide a new improved selectivity of 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 the production of olefins, having a catalyst coke good uniformity and high yield of light olefins, olefins production process better economy 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)相连,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。 [0012] In order to solve the above problems, the present invention provides a methanol and / or dimethyl ether reactor system for olefins, said reaction means comprises a dense phase fluidized bed reactor (2), the cyclone ( 3), stripper (5), riser (7), dense-phase fluidized bed regenerator (10), the cyclone (11), stripper (13) and the riser (15); wherein the reaction filter feed line (I) connected to said dense phase fluidized bed reactor (2) at the bottom; portion of the stripper (5) is in the dense phase fluidized bed reactor (2) among the remaining portion of the dense phase fluidized bed reactor (2) below; said riser (7) is connected to the bottom of the bottom of the stripper (5), said riser (7) and said top secret phase fluidized bed regenerator (10) is connected; regenerator feed line (9) is 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) respectively, the bottom (10) in the remainder of the dense-phase fluidized bed regenerator; the lift with the stripper (13) in the bottom of the tube (15) is connected to the bottom the riser (15) at the top of the dense phase fluidized bed reactor (2) is connected, characterized in that said dense phase fluidized bed reactor (2) and / or dense phase fluidized bed regenerator (10) having a material flow controller (17), said dense phase fluidized bed reactor (2) by the material flow controller (17) is divided into η secondary reaction zone, and the I-th to The first η secondary reaction zone sequentially connected; the dense phase fluidized bed regenerator (10) by the material flow controller (17) is divided into m secondary regeneration zone, and the I-th to the m-th two regeneration zone sequentially connected; and wherein η San 2, m San 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 I-th second reaction zone, the first η secondary reaction zone and the stripper (5) The upper material overflow (18) connected; upper part of the dense phase fluidized bed reactor (2) is provided with a cyclone (3), the cyclone (3) of the top outlet pipe materials and products (4) is connected to the the bottom of the cyclone (3) with the first η secondary reaction zone is 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。 [0014] In a preferred embodiment, the riser (7) on top of the first regeneration zone is connected to two I-th, m-th two regeneration zone and the stripper (13) the upper part of the overflow material port (18) is connected; upper part of the dense phase fluidized bed regenerator (10) is provided with a cyclone (11), the cyclone (11) of the top outlet and an exhaust line (12) is connected to the the bottom of the cyclone (11) is connected to the m-th secondary regeneration zone.

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

[0016] 在一个优选实施方案中,8彡m彡3。 [0016] In a preferred embodiment, eight 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 material flow controller (17) by a partition plate (19), the orifice (20), the material downstream flow tube (21), the bottom of the bezel (22) and the heat removal components (23) the composition; the aperture (20) located below the partition plate (19) and connected to said material downstream flow tube (21) at the bottom, the bottom of the bezel (22) located downstream of the material flow the bottom of the tube (21) and said orifice (20), said heat extraction member (23) fixed to the 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 of the bezel (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) a dense phase fluidized bed with a higher bed density, lower catalyst 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。 [0021] (2) the material flow controller downstream flow tube material gas velocity is less than equal to the minimum fluidization velocity of the catalyst, the catalyst is in the accumulation of dense phase state, forming a dense phase conveying unidirectional flow of catalyst to avoid phase Adjacent the second reaction zone (or adjacent two regeneration zone) between the catalyst back mixing, residence time distribution is 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。 [0022] (3) the material flow controller for heat member having a reaction zone temperature control effect.

[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 material flow controller and the reaction zone divided into η secondary reaction zone, the catalyst I, followed by the second reaction zone to the first η second reaction zone, a narrow residence time distribution, the carbon content of the catalyst to be born greatly improved uniformity.

[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, catalyst I, followed by a secondary regeneration zone to the m-th secondary regeneration zone, a narrow residence time distribution, a uniform carbon content of the regenerated catalyst resistance greatly improved.

[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 the regenerated catalyst and spent catalyst carbon content, and more uniform distribution of the carbon content, improve the selectivity of light olefins, and according to the carbon content of the regulation needs to optimize the propylene / ethylene ratios.

[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, the amount of catalyst required for possession reaction zone is reduced.

[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 of the reactor to facilitate the realization of large-scale.

附图说明 Brief Description

[0028] 图1为本发明所述方法的流程示意图; [0028] FIG. 1 is a schematic flow diagram of the method 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 schematic structural diagram of the dense phase comprising four second reaction zone of the fluidized bed, where AA sectional view of the flow direction of the arrow is 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 view of the invention comprises a structural dense phase four secondary regeneration zone fluidized bed, where BB sectional view of the secondary flow direction arrow is a catalyst regeneration section;

[0031] 图4为本发明所述汽提器的结构示意图; Structure [0031] FIG. 4 of the present invention in 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 is a schematic structural diagram of the invention material flow controller.

[0033] 附图中的附图标记说明如下: [0033] The reference numerals in the accompanying drawings 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 secondary reaction zone feed feeder; 1-2 second leg second reaction zone feed; 1-3 3 second reaction zone feed Extension ; 1-4 4th second reaction zone feed feeder; 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。 2-1 I second reaction zone; the second reaction zone 2 2-2; 2-3 3 second reaction zone; 2_4 4th second reaction zone; 3- cyclone; 4_ product pipeline materials; 5_ stripper; 6_ steam line; 7_ riser; 8_ lift gas pipeline; 9- regenerator feed line; 9_1 regeneration zone I, two feed branch; 9-2 second two regeneration District Extension feed; 9-3 3 two regeneration zone feed feeder; 9_4 fourth two regeneration zone feed feeder; 10_ dense phase fluidized bed regenerator; 10-1 Chapter I two regeneration zone; 10 -2 second regeneration zone two; 10-3 third two regeneration zone; 10-4 fourth two regeneration zone; 11_ cyclones; 12- gas pipeline; 13- stripper; 14- steam pipeline; 15- riser; 16- lift gas pipeline; 17- material flow controller; 18- material overflow; 19_ separator; 20_ orifice; 21_ material downstream flow tube; 22_ bottom of the bezel; 23_ get hot parts.

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 preparation of oxygenates to light olefins selectivity of light olefins in the 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), riser (7), dense-phase fluidized bed regenerator (10), the cyclone (11), stripper (13) and the 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 Connected to the bottom of the reactor feed line (I) and dense-phase fluidized bed reactor (2), the stripper (5) - section (2) in the dense phase fluidized bed reactor, the rest is a dense phase flow connected to the bottom of the fluidized bed reactor (2) below, the steam line (6) and stripper (5), riser (7) of the bottom of the stripper (5) is connected to the bottom of the lift gas pipelines (8 connected to the bottom) and the riser (7), the top of the riser 7 and the dense phase fluidized bed regenerator (10) is connected to the regenerator feed line (9) and dense-phase fluidized bed regenerator (10) of the bottom connected to a portion of the stripper (13) in a dense phase 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 to the bottom of the bottom, steam line (14) and stripper (13), the riser (15) at the bottom of the stripper (13 ) is connected to the bottom of the lift gas line (16) connected to the riser (15) in the bottom of the riser (15) with the top of the dense phase fluidized bed reactor 2) connected (. 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 a reaction zone feed η branch (1-1, ......, 1_η), the dense-phase fluidized bed reactor (2) by the material flow controller ( 17) divided into η secondary reaction zone (2-1, ......, 2-η), η Pie 2, preferably 8 San η Pie 3; η reaction zone feed branch respectively η secondary reaction zone connected; I-th through η secondary reaction zone sequentially connected to the riser (15) is connected to the top of the I-th second reaction zone, the first η secondary reaction zone and stripper (5) the upper part Material overflow port (18) connected to the upper portion of the dense phase fluidized bed reactor (2) is provided with a cyclone (3), the cyclone (3) of the top outlet pipe materials and products (4) is connected to the cyclone bottom (3) with the first η secondary reaction zone is 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, the regenerator feed line (9) includes 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 two m a regeneration zone (10-1, ......, 10-m), m San 2, preferably 8 m San San 3; m a regeneration zone feeds two branch lines, respectively, with the m stage regeneration zone is connected; I-th to the m-th secondary regeneration zone sequentially connected to the riser (7) is connected to the top of the I-th second regeneration zone, the m-th secondary regeneration zone and stripper (13 ) upper part of the overflow gate material (18) is connected to the upper portion of the dense phase fluidized bed regenerator (10) is provided with a cyclone (11), the cyclone (11) of the top outlet and an exhaust line (12) is connected, the bottom of the cyclone (11) is connected to the m-th secondary 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 material flow controller (17) by a partition plate (19), the orifice (20), the material downstream flow tube (21), the bottom of the bezel (22) and the heat removal means (23) consisting 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 orifice (20) located in the separator (19), with the bottom of the down flow tube material (21) is connected to the bottom of the baffle (22) may be non-porous or perforated plate, which is located downstream of material flow tube (21) and a bottom opening (20), to take the heat member (23) is fixed to the spacer (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 according to the invention shown in Figure 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。 Mainly methanol and / or dimethyl ether feed into the dense phase fluidized bed reactor (2), brought into contact with a catalyst to form vapor product stream and spent catalyst, gas product stream and a spent catalyst entrained into the cyclone ( 3), gas product stream through the outlet into the subsequent separation cyclone section, the spent catalyst material entrained by the cyclone leg into the first η secondary reaction zone, the regenerated catalyst through the stripper (13), the riser (15) into the dense phase fluidized bed reactor 2, and sequentially through the first I th to η secondary reaction zone, spent catalyst after the formation of coke, spent catalyst and then through the stripper (5), to enhance the tube (7) into the dense phase fluidized bed regenerator (10), and sequentially through the I-th to the m-th second regeneration zone, after the formation of regenerated catalyst 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 embodiment, the present invention comprises a dense phase fluidized bed of structure 4 second reaction zone diagram shown in Figure 2, AA sectional view of the flow direction of the arrow is the catalyst of the second reaction zone . 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 arranged vertically, the dense phase fluidized bed reaction zone is divided into four second reaction zone, the catalyst sequentially through the I-th to the first four second 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 embodiment, the present invention comprises a dense phase fluidized bed of four secondary structure diagram shown in Figure regeneration zone, BB sectional view of the secondary flow direction arrow is a catalyst regeneration section 3 . 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 arranged vertically, the dense-phase fluidized bed regeneration zone divided into four two regeneration zone, the catalyst sequentially through the I-th through four two 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 stripper (5 and 13) of the present invention, a schematic diagram of the structure shown in Figure 4. 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)。 As the first η stripper opening on the upper part of the wall (5) in a second reaction zone with a stripper (5) between the material overflow outlet (18); stripper opening on the upper part of the wall (13) As a material overflow m-th secondary regeneration zone and 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 structure of the material flow controller of the invention described in the schematic shown in Figure 5. 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 the partition (19), the orifice (20), the material downstream flow tube (21), the bottom of the bezel (22) and take the heat member (23) component. 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)。 By the downward flow of catalyst material over the tube into the downstream flow tube, wherein the gas superficial linear velocity is less than equal to the minimum fluidization velocity, catalyst material downstream flow tube in dense phase deposition state, forming materials flow driving force, a catalyst for the inflow orifice through which After the second reaction zone (or regeneration zone). 取热部件可采用盘管结构,固定于隔板之上。 Take hot parts coil structure 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个二级再生区至第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 [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; material flow controller within the gas superficial linear velocity of less than or equal catalysts the minimum fluidization velocity; preferably said catalyst comprises a SAPO molecular sieve catalyst, more preferably a molecular sieve catalyst comprising SAP0-34; located at the bottom of the reaction zone There feed, feed including methanol and / or dimethyl ether and the like; the stripper (13) stripping medium containing water vapor; the regeneration zone (10) is provided at the bottom of the regeneration medium inlet, the regeneration medium comprises air, oxygen-depleted air, water vapor and the like; the reaction zone (2) of the reaction temperature is 400-550 ° C, the bed density 200-1200kg / m3, the average amount of coke from the catalyst I, a second reaction zone through η secondary reaction zone in ascending order, the average amount of coke I, secondary reaction zone is 0.5-3wt%, the average amount of the first η coke secondary reaction zone 7-10wt%; the regeneration zone (10) of the reaction temperature is 500-700 ° C, the bed density 200-1200kg / m3, the average amount of coke from the catalyst I, secondary regeneration zone to the regeneration zone m-th two descending, Part I The average amount of coke for the secondary regeneration zone

3-10wt%,第m个二级再生区的平均积炭量为0-3wt%。 3-10wt%, the average amount of the m-th secondary coke 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 may be to control the amount of carbon catalyst, to improve the uniformity of the carbon content and the purpose of improving the selectivity of light olefins, with great technical advantages, it can be used for industrial production of light 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] In order to better illustrate the present invention, to facilitate understanding the technical aspect of the present invention, the present invention is typical but non-limiting embodiment, 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] Set within the dense phase fluidized bed reactor 4 second reaction zone, set up four secondary regeneration zone within the dense phase fluidized bed regenerator, mainly methanol and / or dimethyl ether of raw materials into the dense phase flow bed reactor with a molecular sieve catalyst comprising contacting SAP0-34 resulting vapor product stream and spent catalyst, gas and spent catalyst material entrained into the cyclone, gas product stream through the outlet into the subsequent separation cyclone section, entrained spent catalyst material by cyclone leg into the first four 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。 After the regenerated catalyst stripper, riser into the dense phase fluidized bed reactor, and sequentially through the I-th to 4 second reaction zone, spent catalyst after the formation of coke, spent catalyst stripper and then after, riser into the dense phase fluidized bed regenerator, and sequentially through the I-th to 4 secondary regeneration zone, after the formation of regenerated catalyst 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%。 Dense phase fluidized bed reactor reaction conditions: reaction temperature of 400 ° C, Gas linear velocity of 0.3m / s, the bed density of 1000kg / m3, the average amount of coke I, secondary reaction zone is 2wt% The average coke in Section 2 the second reaction zone is 6wt%, the average coke in Section 3 second reaction zone is 8wt%, the average coke in Section 4 second reaction zone is 1wt%; close phase fluidized bed regenerator reaction conditions: reaction temperature of 500 ° C, Gas linear velocity of 0.3m / s, the bed density of 1000kg / m3, the average amount of coke I of secondary regeneration zone is 7wt%, The average amount of the first two secondary coke regeneration zone is 4wt%, the average amount of the first three secondary coke regeneration zone is 2wt%, the average coke in Section 4 second regeneration zone is 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 on-line gas chromatographic analysis, the carbon-based olefins yield 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] Set within the dense phase fluidized bed reactor 3 second reaction zone, set up two second regeneration zone within the dense phase fluidized bed regenerator, mainly methanol and / or dimethyl ether of raw materials into the dense phase flow bed reactor with a molecular sieve catalyst comprising contacting SAP0-34 resulting vapor product stream and spent catalyst, gas and spent catalyst material entrained into the cyclone, gas product stream through the outlet into the subsequent separation cyclone section, entrained spent catalyst material through the cyclone 3 into the first two legs of the 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。 After the regenerated catalyst stripper, riser into the dense phase fluidized bed reactor, and sequentially through the I-th to 3 second reaction zone, spent catalyst after the formation of coke, spent catalyst stripper and then after, riser into the dense phase fluidized bed regenerator, and I sequentially through the first two months to two regeneration zone, after the formation of regenerated catalyst 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%。 Dense phase fluidized bed reactor reaction conditions: reaction temperature is 450 ° C, Gas linear velocity of 0.5m / s, the bed density of 900kg / m3, the average amount of coke I, secondary reaction zone is 3wt% The average coke in Section 2 the second reaction zone is 7wt%, the average amount of coke third secondary reaction zone 9wt%; dense phase fluidized bed regenerator reaction 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 of secondary regeneration zone is 4wt%, the average amount of the first two 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 on-line gas chromatographic analysis, the carbon-based olefins yield 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] Set within the dense phase fluidized bed reactor 6 second reaction zone, set up five secondary regeneration zone within the dense phase fluidized bed regenerator, mainly methanol and / or dimethyl ether of raw materials into the dense phase flow bed reactor with a molecular sieve catalyst comprising contacting SAP0-34 resulting vapor product stream and spent catalyst, gas and spent catalyst material entrained into the cyclone, gas product stream through the outlet into the subsequent separation cyclone section, entrained spent catalyst material by cyclone leg into the first six 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。 After the regenerated catalyst stripper, riser into the dense phase fluidized bed reactor, and sequentially through I-6 second reaction zone, after the formation of carbon spent catalyst, spent catalyst stripper and then after upgrade tube into the dense phase fluidized bed regenerator, and sequentially through I-5 second regeneration zone, after the formation of regenerated catalyst 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%。 Dense phase fluidized bed reactor reaction conditions: reaction temperature of 480 ° C, Gas linear velocity of 0.7m / s, the bed density of 700kg / m3, the average amount of coke I, secondary reaction zone lwt% The average coke in Section 2 the second reaction zone is 3wt%, the average coke in Section 3 second reaction zone is 4wt%, the average coke in Section 4 second reaction zone is 5wt%, the first The average amount of coke 5 second reaction zone is 6wt%, the average coke in Section 6 second reaction zone 7wt%; dense phase fluidized bed regenerator reaction conditions: reaction temperature of 650 ° C, Gas The line speed was l.0m / s, the bed density of 500kg / m3, the average amount of coke I of secondary regeneration zone to 5wt%, the average amount of the second secondary coke regeneration zone to 3wt%, the first The average amount of coke three secondary regeneration zone is 2wt%, the average coke in Section 4 second regeneration zone is lwt%, the average coke in Section 5 second regeneration zone was 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 on-line gas chromatographic analysis, the carbon-based olefins yield 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。 Above [0051] The present invention has 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 may be made other changes and modifications. 本发明的范围由所附权利要求限定。 The scope of the invention defined by the appended claims.

Citas de patentes
Patente citada Fecha de presentación Fecha de publicación Solicitante Título
CN101239871A *7 Feb 200713 Ago 2008中国石油化工股份有限公司Method for increasing selectivity of low-carbon olefins in methanol or dimethyl ether converting process
CN101698629A *4 Nov 200928 Abr 2010兆威兴业有限公司Device for preparing low-carbon olefin by adopting methanol or dimethyl ether
CN103193574A *10 Ene 201210 Jul 2013中国石油化工股份有限公司On-stream method of methanol to light olefin reaction-regeneration device
US6166282 *20 Ago 199926 Dic 2000Uop LlcFast-fluidized bed reactor for MTO process
Clasificaciones
Clasificación internacionalC07C1/20, C07C11/06, B01J8/26, C07C11/04
Clasificación cooperativaY02P30/42
Eventos legales
FechaCódigoEventoDescripción
3 Jun 2015C06Publication
1 Jul 2015C10Entry into substantive examination
8 Jun 2016C14Grant of patent or utility model