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MTO reaction - regeneration means

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Publication number
CN102276400A
CN102276400A CN 201010199977 CN201010199977A CN102276400A CN 102276400 A CN102276400 A CN 102276400A CN 201010199977 CN201010199977 CN 201010199977 CN 201010199977 A CN201010199977 A CN 201010199977A CN 102276400 A CN102276400 A CN 102276400A
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conveying
reactor
methanol
product
regenerator
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CN 201010199977
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Chinese (zh)
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CN102276400B (en )
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张惠明
王洪涛
钟思青
齐国祯
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中国石油化工股份有限公司
中国石油化工股份有限公司上海石油化工研究院
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    • 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
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/50Improvements relating to the production of products other than chlorine, adipic acid, caprolactam, or chlorodifluoromethane, e.g. bulk or fine chemicals or pharmaceuticals
    • Y02P20/52Improvements relating to the production of products other than chlorine, adipic acid, caprolactam, or chlorodifluoromethane, e.g. bulk or fine chemicals or pharmaceuticals using catalysts, e.g. selective catalysts
    • 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
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/50Improvements relating to the production of products other than chlorine, adipic acid, caprolactam, or chlorodifluoromethane, e.g. bulk or fine chemicals or pharmaceuticals
    • Y02P20/58Recycling
    • Y02P20/584Recycling of catalysts
    • 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 low carbon olefin reaction-regeneration device by using methanol, which mainly solves the problem of low yield of low carbon olefin in the reaction-regeneration device in the prior art. The low carbon olefin reaction-regeneration device by using methanol comprises a methanol conveying reactor 3, a by-product conveying reactor 11, a regenerator 18, an overflow pipe 12 and a lifting pipe 10, the upper part of the by-product conveying reactor 11 is connected with the regenerator 18, the lower part of the by-product conveying reactor 11 is connected with the methanol conveying reactor 3, a degassing zone 20 is provided in the regenerator 18, a catalyst in the degassing zone 20 is entered into the by-product conveying reactor 11 through the overflow pipe 12, a catalyst outlet is opened at the lower part of the by-product conveying reactor 11 and is connected with the methanol conveying reactor 3 through the catalyst conveying tube 5, a stripping zone 6 is provided in the methanol conveying reactor 3, a catalyst in the stripping zone 6 is entered into the regenerator 18 through the lifting pipe 10, a product outlet is opened at the upper part of the methanol conveying reactor 3 and the by-product conveying reactor 11, the problem is better solved by the present invention by the technical scheme that the fume outlet is opened at the top of the regenerator 18. The present invention can be used for the industrial production of low carbon olefin.

Description

甲醇制低碳烯烃反应-再生装置 MTO reaction - regeneration means

技术领域 FIELD

[0001] 本发明涉及一种甲醇制低碳烯烃反应-再生装置。 [0001] The present invention relates to an MTO reactor - reproducing apparatus. 技术背景 technical background

[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. 其中,一类重要的用于轻质烯烃生产的替代原料是含氧化合物,例如醇类(甲醇、乙醇)、醚类(二甲醚、甲乙醚)、酯类(碳酸二甲酯、甲酸甲酯)等,这些含氧化合物可以通过煤、天然气、生物质等能源转化而来。 Wherein, an important class of alternative raw materials for the production of light olefins are oxygenates, such as alcohols (methanol, ethanol), ethers (dimethyl ether, methyl ethyl ether), esters (dimethyl carbonate, methyl formate esters), these may be converted from an oxygenate by coal, natural gas, biomass and other energy. 某些含氧化合物已经可以达到较大规模的生产,如甲醇,可以由煤或天然气制得,工艺十分成熟,可以实现上百万吨级的生产规模。 Certain oxygenates have large-scale production can be achieved, such as methanol, may be obtained from coal or natural gas, very mature technology, can be implemented on a production scale megaton. 由于含氧化合物来源的广泛性,再加上转化生成轻质烯烃工艺的经济性,所以由含氧化合物转化制烯烃(OTO)的工艺,特别是由甲醇转化制烯烃(MTO)的工艺受到越来越多的重视。 Because of the extensive source oxygenate, together with conversion of light olefins to generate economic process, so the process to olefins (the OTO) conversion of the oxygenates, in particular by the conversion of methanol to olefins (MTO) process more to more attention.

[0003] US4499327专利中对磷酸硅铝分子筛催化剂应用于甲醇转化制烯烃工艺进行了详细研究,认为SAP0-34是MTO工艺的首选催化剂。 [0003] US4499327 patent applied for the conversion of methanol to olefins process silicoaluminophosphate zeolite catalysts were studied in detail, the preferred catalyst SAP0-34 that the MTO process. SAP0-34催化剂具有很高的轻质烯烃选择性,而且活性也较高,可使甲醇转化为轻质烯烃的反应时间达到小于10秒的程度,更甚至达到提升管的反应时间范围内。 SAP0-34 catalyst having a high light olefin selectivity, but the activity is higher, the conversion of methanol to light olefins allows the reaction time to the extent of less than 10 seconds, even more time to reach the reaction riser.

[0004] US6166282中公布了一种氧化物转化为低碳烯烃的技术和反应器,采用快速流化床反应器,气相在气速较低的密相反应区反应完成后,上升到内径急速变小的快分区后,采用特殊的气固分离设备初步分离出大部分的夹带催化剂。 [0004] US6166282 discloses a the conversion of oxygenates to light olefins and reactor technology, the use of a fast fluidized bed reactor, after completion of the reaction gas in the lower gas velocity dense phase reaction zone, rising to rapidly change the inner diameter fast after a small partition, gas-solid separation apparatus using special preliminary separation of the majority of entrained catalyst. 由于反应后产物气与催化剂快速分离,有效的防止了二次反应的发生。 Since the reaction product gas after the rapid separation of the catalyst, effectively prevents the occurrence of secondary reactions. 经模拟计算,与传统的鼓泡流化床反应器相比,该快速流化床反应器内径及催化剂所需藏量均大大减少。 Simulated calculation, compared with the conventional bubbling fluidized bed reactor, a fast fluidized bed of the desired inner diameter of the reactor volume and catalyst inventory is greatly reduced.

[0005] CN1723^52中公布了带有中央催化剂回路的多级提升管反应装置用于氧化物转化为低碳烯烃工艺,该套装置包括多个提升管反应器、气固分离区、多个偏移元件等,每个提升管反应器各自具有注入催化剂的端口,汇集到设置的分离区,将催化剂与产品气分开。 [0005] CN1723 ^ 52 published a multistage reaction apparatus for riser oxide catalyst with a central loop into light olefins process, the set of devices comprises a plurality of riser reactors, gas-solid separation zone, a plurality of offset components, etc., each having a respective riser reactor catalyst injection port, to a separation zone provided together, the catalyst is separated from the product gas.

[0006] 本领域所公知的,要保证高的低碳烯烃选择性,催化剂上需要一定数量的积碳,而且甲醇转化为低碳烯烃的过程中对反应温度等工艺参数十分敏感。 [0006] This known in the art, to ensure a high selectivity to light olefins, a certain amount of coke on the catalyst, and the conversion of methanol to light olefins during the reaction process parameters such as temperature sensitive. 现有技术均存在由于反应区内催化剂积炭分布不均、反应温度波动大而导致的低碳烯烃收率较低的问题。 Exist in the prior art lower olefins yield problems due to uneven distribution of the catalyst coke within the reaction zone, the reaction temperature fluctuation caused. 另外,在甲醇制备低碳烯烃的过程中,不可避免的会产生某些副产物,如碳四以上烃等,若将这些副产物进一步转化为目的产物,将会提高低碳烯烃的收率和工艺经济性。 Further, during the preparation of light olefins in methanol, inevitably produces some byproducts, such as four or more carbon hydrocarbons, etc., when these byproducts further converted to the desired product, will increase the yield of light olefins and process economics. 本发明有针对性的解决了上述问题。 It has targeted the present invention solves the above problem.

发明内容 SUMMARY

[0007] 本发明所要解决的技术问题是现有技术中存在的低碳烯烃收率不高的问题,提供一种新的甲醇制低碳烯烃反应-再生装置。 [0007] The present invention solves the technical problem of the prior art lower olefin yields present not high, to provide a new MTO reaction - regeneration means. 该装置用于低碳烯烃的生产中,具有低碳烯烃收率较高的优点。 The apparatus for producing lower olefins, having the advantage of higher yields of light olefins. [0008] 为解决上述问题,本发明采用的技术方案如下:一种甲醇制低碳烯烃反应-再生装置,主要包括甲醇转化反应器3、副产物转化反应器11、再生器18、溢流管12、提升管10, 副产物转化反应器11上部与再生器18相连,下部与甲醇转化反应器3相连,再生器18内部设有脱气区20,脱气区20内催化剂通过溢流管12进入副产物转化反应器11,副产物转化反应器11下部开有催化剂出口,通过催化剂输送管5与甲醇转化反应器3相连,甲醇转化反应器3内部设有汽提区6,汽提区6内催化剂通过提升管10进入再生器18,甲醇转化反应器3和副产物转化反应器11上部开有产品出口,再生器18顶部开有烟气出口。 [0008] In order to solve the above problems, the present invention adopts the technical solution as follows: A MTO reactor - reproducing apparatus including methanol conversion reactor 3, byproduct conversion reactor 11, a regenerator 18, an overflow pipe 12, riser 10, byproducts conversion reactor 11 is connected to the upper portion of regenerator 18, the lower portion 3 is connected to the methanol conversion reactor, the regenerator 18 is provided with internal degassing zone 20, the catalyst 20 within the degassing zone through the overflow pipe 12 the product was converted into the secondary reactor 11, the lower portion of the reactor byproducts conversion catalyst outlet opening 11, connected through the catalyst feed pipe 5 and the methanol conversion reactor 3, the methanol conversion reactor 3 is provided inside the stripping zone 6, the stripping zone 6 the catalyst enters regenerator 10 through the riser 18, the methanol conversion reactor 3 and byproduct conversion reactor upper product outlet 11 is opened, the top of the regenerator flue gas outlet 18 is opened.

[0009] 上述技术方案中,所述催化剂包括SAP0-34分子筛;所述产品出口和烟气出口前均设置气固旋风分离器;所述脱气区20脱气介质选自水蒸气,汽提区6汽提介质选自水蒸气,提升管10提升介质选自水蒸气;所述再生器18通过内置取热器控制再生温度;所述甲醇转化反应器3可设置外置或内置取热器控制反应温度;所述脱气区20和汽提区6侧壁上部开有至少一个催化剂入口;所述副产物转化反应器11产品和甲醇转化反应器3产品共用一套分离流程;所述副产物为碳四〜碳六混合烃;所述混合烃中碳四烃质量含量大于80 %,烯烃质量含量大于60 %。 [0009] In the above technical solution, the catalyst comprising a molecular sieve SAP0-34; a cyclone gas-solid products are arranged before the outlet and a flue gas outlet; degassing zone 20 of the degassing medium is selected from water vapor, stripped region 6 is selected from steam stripping medium, medium lift riser 10 is selected from steam; regenerator 18 controls the regeneration temperature by the built-in heat remover; the methanol conversion reactor 3 may be arranged external or internal heat extractor controlling the reaction temperature; the sidewalls of the upper portion 6 and a degassing zone stripping zone 20 is opened at least one catalyst inlet; the byproduct conversion reactor 11 and product methanol conversion reactor 3 products share a separation process; the secondary 4- to 6 carbon product is carbon mixed hydrocarbons; said hydrocarbon mass mixed hydrocarbon content of greater than 80% tetrakis olefin content greater than 60% by mass.

[0010] 甲醇制低碳烯烃反应过程中不可避免的会产生碳四以上烃等副产物,这部分副产物产率高、且烯烃含量高,通过研究发现,这部分烯烃含量很高的碳四以上混合烃是很好的生产低碳烯烃的原料。 [0010] MTO reaction process inevitably generates more than four carbon byproduct hydrocarbons, this part of the by-product yield and a high olefin content, the study found that this part of the high olefin content carbon four above mixed hydrocarbon feedstock is a good production of light olefins. 采用本发明的方法,设置一个副产物转化器,主要用于转化甲醇制低碳烯烃过程中形成的碳四〜碳六烃副产物,用于增产低碳烯烃。 Using the method of the invention, it is provided a byproduct reformer, the carbon is mainly used for the 4th and byproduct carbon hexamethonium MTO conversion process is formed for light olefins yield. 副产物转化器的催化剂直接来自再生器,有利于保证碳四以上烃转化所需的反应温度和催化剂活性。 By-products directly from the reformer catalyst regenerator will help to ensure the reaction temperature and catalyst activity more than four carbon hydrocarbon conversion desired. 本发明人通过研究发现,碳四以上烃转化会在催化剂上生成积碳,而生成的积碳显著提高了催化剂的选择性,有利于甲醇高选择性的生产低碳烯烃。 The present inventors found that the hydrocarbon conversion generates more than four carbon coke on the catalyst, and the resulting carbon significantly improves the selectivity of the catalyst, methanol favor high selectivity to light olefins. 同时,高温再生催化剂通过副产物转化器后, 温度有所降低,相应减少了甲醇转化反应器的取热负荷。 Meanwhile, the high temperature regenerated catalyst from the conversion by-products, the temperature decreased, a corresponding reduction in the heat removal load of methanol conversion reactor. 另外,现有技术一般均采用反应器、再生器并列布置,占地空间较大、催化剂输送管路较长。 Further, the prior art generally use a reactor, a regenerator arranged in parallel, a large floor space, longer catalyst delivery line. 本发明中采用再生器、副产物转化器、甲醇转化反应器同轴布置,大大减少了传统反应-再生装置的占地空间,同时催化剂输送管路大大缩短。 The present invention is employed in the regenerator, byproduct reformer, the methanol conversion reactor arranged coaxially, greatly reducing the conventional reactor - footprint reproducing apparatus, while greatly reducing the catalyst transfer line.

[0011] 采用本发明的技术方案:所述催化剂包括SAP0-34分子筛;所述产品出口和烟气出口前均设置气固旋风分离器;所述脱气区20脱气介质选自水蒸气,汽提区6汽提介质选自水蒸气,提升管10提升介质选自水蒸气;所述再生器18通过内置取热器控制再生温度; 所述甲醇转化反应器3可设置外置或内置取热器控制反应温度;所述脱气区20和汽提区6侧壁上部开有至少一个催化剂入口;所述副产物转化反应器11产品和甲醇转化反应器3产品共用一套分离流程;所述副产物为碳四〜碳六混合烃;所述混合烃中碳四烃质量含量大于80%,烯烃质量含量大于60%,甲醇转化反应器出口产品中低碳烯烃碳基收率达到80. 67% (重量),副产物转化反应器出口产品中低碳烯烃收率达到35. 47% (重量),取得了较好的技术效果。 [0011] The technical solution of the present invention: the catalyst comprises a molecular sieve SAP0-34; a cyclone gas-solid products are arranged before the outlet and a flue gas outlet; degassing zone 20 of the degassing medium is selected from water vapor, stripping zone 6 is selected from steam stripping medium, medium lift riser 10 is selected from steam; regenerator 18 controls the regeneration temperature by the built-in heat remover; the methanol conversion reactor 3 may be arranged external or internal to take controlling the reaction temperature heat; the sidewalls of the upper portion 6 and a degassing zone stripping zone 20 is opened at least one catalyst inlet; the byproduct conversion reactor 11 and product methanol conversion reactor 3 products share a separation process; the said by-product carbon 4- to 6 carbon mixed hydrocarbons; said hydrocarbon mixed hydrocarbon four carbon content of greater than 80 mass% olefin content greater than 60% by mass, a carbon-based methanol conversion yield of light olefins at the reactor outlet the product 80. 67% (by weight), by-product in the conversion reactor outlet product olefins yield of 35.47% (by weight), and achieved good results in the art.

附图说明 BRIEF DESCRIPTION

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

[0013] 图1中,1为提升管提升介质进料;2为汽提介质进料;3为甲醇转化反应器;4为甲醇原料进料;5为催化剂输送管;6为汽提区;7为汽提区侧壁催化剂入口;8为反应器外取热器;9为气固旋风分离器;10为提升管;11为副产物转化反应器;12为溢流管;13为气固旋风分离器;14为副产物进料;15为产品出口;16为集气室;17为再生介质进料;18为再生器;19为脱气介质进料;20为脱气区;21为再生器取热器;22为气固旋风分离器;23为烟气出口。 In [0013] FIG. 1, 1 is a riser lift medium feed; 2 as stripping medium feed; 3 methanol conversion reactor; 4 methanol feedstock feed; 5 catalyst delivery tube; 6 is a stripping zone; 7 is a side wall of the catalyst stripping zone inlet; 8 outer reactor heat extractor; gas-solid cyclone 9; 10 to a riser; 11 byproduct of the conversion reactor; overflow pipe 12; 13 to gas-solid cyclone; a byproduct feed 14; 15 for the product outlet; plenum 16; 17 to feed the regeneration medium; the regenerator 18; 19 deaerated feed medium; degassing zone 20; 21 The regenerator heat remover; 22 is a gas-solid cyclone; flue gas outlet 23.

[0014] 原料经进料管线4进入甲醇转化反应器3中,与分子筛催化剂接触,反应生成含有低碳烯烃的产品,经过气固快速分离设备9分离后进入集气室16,失活催化剂经过汽提区6 汽提后通过提升管10进入再生器18再生,再生催化剂通过溢流管12进入副产物转化反应器11中,与碳四以上烃等副产物接触,生成的产品经过气固旋风分离器13分离后进入集气室,副产物转化反应器内的催化剂通过催化剂输送管5进入甲醇转化反应器3中,继续与甲醇反应。 [0014] The starting material through the feed line 4 to the methanol conversion reactor 3, in contact with a molecular sieve catalyst, reaction product containing light olefins, after separating apparatus Solid Separator 9 enters the plenum chamber 16, through the deactivation of the catalyst after stripping the stripping zone 6 via the riser 10 into the regenerator 18, and the regeneration of the catalyst by-products into the overflow pipe 11 in the conversion reactor 12, in contact with four or more carbon byproduct hydrocarbon, the resulting product through a gas-solid cyclone after separation of the separator 13 into the plenum byproduct reforming catalyst in the reactor tube 5 to the methanol conversion reactor 3, via reaction with methanol to continue catalyst delivery.

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

具体实施方式 detailed description

[0016]【实施例1】 [0016] [Example 1]

[0017] 在如图1所示的反应-再生装置中,只是未设置集气室,甲醇转化反应器产品和副产物转化反应器产品分开在线分析。 [0017] In the reaction shown in Figure 1 - reproducing apparatus, only the plenum chamber is not provided, the methanol conversion reactor products and byproducts separate conversion reactor product line analysis. 甲醇转化反应器的平均温度为450°C,床层密度为170 千克/立方米,副产物转化反应器的平均温度为552°C,床层密度为220千克/立方米。 The average temperature of the methanol conversion reactor of 450 ° C, the bed density of 170 kg / m3 with a mean temperature conversion reactor byproducts to 552 ° C, the bed density of 220 kg / m3. 反应-再生系统压力为常压,甲醇转化反应器以纯度为99. 5%的甲醇进料,进料为1千克/小时,催化剂为SAP0-34,汽提区汽提介质、脱气区脱气介质、提升管提升介质均为水蒸气,再生器设置内取热盘管控制再生温度,再生温度为674°C。 The reaction - regeneration system to atmospheric pressure, methanol conversion reactor having a purity of 99.5% methanol feed, the feed was 1 kg / hr, the catalyst is SAP0-34, stripping medium stripping zone, a degassing zone off gas medium lift riser media are steam, heat removal coil disposed within the regenerator temperature control regeneration, regeneration temperature of 674 ° C. 副产物转化反应器进料为碳四以上混合烃,其中碳四烃质量含量为91%,烯烃质量含量为87%,再生催化剂积碳量为0. 47%, 从副产物转化反应器中出来的催化剂积碳量为1.6%,保持催化剂流动控制的稳定性,反应器出口产物均采用在线气相色谱分析,甲醇转化反应器出口产品中低碳烯烃碳基收率为80.67% (重量),副产物转化反应器出口产品中低碳烯烃收率为35.47% (重量)。 Byproduct conversion reactor feed is mixed more than four carbon hydrocarbons, wherein the carbon Hydrocarbon content was 91% by mass, the olefin content of 87% by mass, the regeneration of the catalyst in an amount of 0.47% carbon, up conversion reactor byproducts from carbon catalyst in an amount of 1.6%, to maintain the stability of the control flow of the catalyst, the reactor outlet products were analyzed using online gas chromatography, the methanol conversion reactor outlet carbon-based products in a yield of lower olefins 80.67% (by weight), sub converting the product outlet of the reactor product olefins yield 35.47% (by weight).

[0018]【实施例2】 [0018] [Example 2]

[0019] 按照实施例1所述的条件,副产物转化反应器进料为碳四以上混合烃,其中碳四烃质量含量为80%,烯烃质量含量为60%,再生催化剂积碳量为0. 27%,从副产物转化反应器中出来的催化剂积碳量为1. 18%,保持催化剂流动控制的稳定性,反应器出口产物均采用在线气相色谱分析,甲醇转化反应器出口产品中低碳烯烃碳基收率为80. 48% (重量),副产物转化反应器出口产品中低碳烯烃收率为30. 61% (重量)。 [0019] under the conditions described in Example 1, the byproduct conversion reactor feed is mixed more than four carbon hydrocarbons, wherein the carbon Hydrocarbon content of 80% by mass, the olefin content of 60% by mass, the amount of carbon catalyst regeneration is 0 27% carbon conversion the amount of catalyst in the reactor out of the by-product was 1.18%, to maintain the stability of the control flow of the catalyst, the reactor outlet products were analyzed using online gas chromatography, the methanol conversion in the reactor outlet products low olefin based carbon-carbon yield of 80.48% (by weight), by-product in the conversion reactor outlet product olefins yield 30.61% (by weight).

[0020]【比较例1】 [0020] [Comparative Example 1]

[0021] 按照实施例1所述的条件,不设副产物转化反应器,再生催化剂直接返回到甲醇转化反应器下部,低碳烯烃碳基收率为79. 63%重量。 [0021] in accordance with conditions of the direct return to Example 1, no byproducts conversion reactor, the regenerated catalyst to a lower conversion reactor, the carbon-based lower olefin yield 79.63% by weight of methanol.

[0022] 显然,采用本发明的方法,可以达到提高低碳烯烃收率的目的,具有较大的技术优势,可用于低碳烯烃的工业生产中。 [0022] Obviously, the present invention method, the purpose of improving the yield of light olefins, with great technical advantages, can be used for industrial production of lower olefins.

Claims (10)

1. 一种甲醇制低碳烯烃反应-再生装置,主要包括甲醇转化反应器(3)、副产物转化反应器(11)、再生器(18)、溢流管(12)、提升管(10),副产物转化反应器(11)上部与再生器(18)相连,下部与甲醇转化反应器C3)相连,再生器(18)内部设有脱气区(20),脱气区(20)内催化剂通过溢流管(1¾进入副产物转化反应器(11),副产物转化反应器(11)下部开有催化剂出口,通过催化剂输送管(5)与甲醇转化反应器(3)相连,甲醇转化反应器(3) 内部设有汽提区(6),汽提区(6)内催化剂通过提升管(10)进入再生器(18),甲醇转化反应器(3)和副产物转化反应器(11)上部开有产品出口,再生器(18)顶部开有烟气出口。 An MTO reaction - regeneration apparatus including methanol conversion reactor (3), by-product conversion reactor (11), the regenerator (18), the overflow pipe (12), the riser (10 ), byproduct conversion reactor (11) and the upper portion of the regenerator (18) is connected with a lower methanol conversion reactor C3) is connected to the regenerator (18) is provided with internal degassing zone (20), the degassing zone (20) the catalyst is prepared by the overflow pipe (1¾ byproducts into the conversion reactor (11), by-product conversion reactor (11) a lower outlet opening and a catalyst through a catalyst feed pipe (5) with a methanol conversion reactor (3) is connected, methanol conversion reactor (3) is provided inside the stripping zone (6), within the stripping zone (6) into the catalyst regenerator (18) through a riser (10), the methanol conversion reactor (3) and the by-product conversion reactor (11) has an upper product outlet opening, the regenerator (18) has a top flue gas outlet opening.
2.根据权利要求1所述甲醇制低碳烯烃反应-再生装置,其特征在于所述催化剂包括SAP0-34分子筛。 2. The method of claim 1 MTO reactor - reproducing apparatus, characterized in that said catalyst comprises a molecular sieve SAP0-34.
3.根据权利要求1所述甲醇制低碳烯烃反应-再生装置,其特征在于所述产品出口和烟气出口前均设置气固旋风分离器。 1 according to the MTO reactor as claimed in claim - reproducing apparatus, wherein a gas-solid cyclone separators are disposed before the flue gas outlet and a product outlet.
4.根据权利要求1所述甲醇制低碳烯烃反应-再生装置,其特征在于所述脱气区00) 脱气介质选自水蒸气,汽提区(6)汽提介质选自水蒸气,提升管(10)提升介质选自水蒸气。 1 according to the MTO reactor as claimed in claim - reproducing apparatus, characterized in that the degassing zone 00) degassed medium is selected from water vapor, stripping zone (6) is selected from steam stripping medium, riser (10) to enhance the medium is selected from water vapor.
5.根据权利要求1所述甲醇制低碳烯烃反应-再生装置,其特征在于所述再生器(18) 通过内置取热器控制再生温度。 1 according to the MTO reactor as claimed in claim - reproducing means, wherein said regenerator (18) controlled by a built-regeneration temperature heat extractor.
6.根据权利要求1所述甲醇制低碳烯烃反应-再生装置,其特征在于所述甲醇转化反应器C3)可设置外置或内置取热器控制反应温度。 1 according to the MTO reactor as claimed in claim - reproducing apparatus, characterized in that the methanol conversion reactor C3) may be arranged external or internal heat extraction control the reaction temperature.
7 根据权利要求1所述甲醇制低碳烯烃反应-再生装置,其特征在于所述脱气区00) 和汽提区(6)侧壁上部开有至少一个催化剂入口。 7 according to the MTO reactor 1 as claimed in claim - reproducing apparatus, characterized in that the degassing zone 00) and the stripping zone (6) to open the upper portion of the side wall with at least one catalyst inlet.
8.根据权利要求1所述甲醇制低碳烯烃反应-再生装置,其特征在于所述副产物转化反应器(11)产品和甲醇转化反应器(3)产品共用一套分离流程。 1 according to the MTO reactor as claimed in claim - reproducing apparatus, wherein the byproduct conversion reactor (11) and product methanol conversion reactor (3) a common product separation schemes.
9.根据权利要求1所述甲醇制低碳烯烃反应-再生装置,其特征在于所述副产物为碳四〜碳六混合烃。 1 according to the MTO reactor as claimed in claim - reproducing apparatus, wherein the byproduct is a 4- to six carbon mixed hydrocarbon carbon.
10.根据权利要求9所述甲醇制低碳烯烃反应-再生装置,其特征在于所述混合烃中碳四烃质量含量大于80 %,烯烃质量含量大于60 %。 According to claim 9 MTO reaction requires - reproducing apparatus, wherein said mixed hydrocarbon Hydrocarbon carbon content greater than 80% by mass, the olefin content greater than 60% by mass.
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102872770A (en) * 2011-07-12 2013-01-16 中国石油化工股份有限公司 Reaction unit for preparing low-carbon olefins
CN103537235A (en) * 2012-07-12 2014-01-29 中国石油化工股份有限公司 Reaction device for preparing low-carbon olefin by using oxy-compounds

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6166282A (en) * 1999-08-20 2000-12-26 Uop Llc Fast-fluidized bed reactor for MTO process
CN1962573A (en) * 2006-12-01 2007-05-16 中国化学工程集团公司 Method and reactor for catalytic cracking for producing propylene using fluid bed
CN101402538A (en) * 2008-11-21 2009-04-08 中国石油化工股份有限公司;中国石油化工股份有限公司上海石油化工研究院 Method for improving yield of light olefins

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6166282A (en) * 1999-08-20 2000-12-26 Uop Llc Fast-fluidized bed reactor for MTO process
CN1962573A (en) * 2006-12-01 2007-05-16 中国化学工程集团公司 Method and reactor for catalytic cracking for producing propylene using fluid bed
CN101402538A (en) * 2008-11-21 2009-04-08 中国石油化工股份有限公司;中国石油化工股份有限公司上海石油化工研究院 Method for improving yield of light olefins

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102872770A (en) * 2011-07-12 2013-01-16 中国石油化工股份有限公司 Reaction unit for preparing low-carbon olefins
CN102872770B (en) * 2011-07-12 2015-04-08 中国石油化工股份有限公司 Reaction unit for preparing low-carbon olefins
CN103537235A (en) * 2012-07-12 2014-01-29 中国石油化工股份有限公司 Reaction device for preparing low-carbon olefin by using oxy-compounds
CN103537235B (en) * 2012-07-12 2016-04-13 中国石油化工股份有限公司 Oxygenate to olefins reaction unit

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