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Número de publicaciónCN102276400 A
Tipo de publicaciónSolicitud
Número de solicitudCN 201010199977
Fecha de publicación14 Dic 2011
Fecha de presentación11 Jun 2010
Fecha de prioridad11 Jun 2010
También publicado comoCN102276400B
Número de publicación201010199977.2, CN 102276400 A, CN 102276400A, CN 201010199977, CN-A-102276400, CN102276400 A, CN102276400A, CN201010199977, CN201010199977.2
Inventores张惠明, 王洪涛, 钟思青, 齐国祯
Solicitante中国石油化工股份有限公司, 中国石油化工股份有限公司上海石油化工研究院
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Enlaces externos:  SIPO, Espacenet
甲醇制低碳烯烃反应-再生装置 MTO reaction - reproducing apparatus traducido del chino
CN 102276400 A
Resumen
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.
Reclamaciones(10)  traducido del chino
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 means, including methanol conversion reactor (3), by-product conversion reactor (11), the regenerator (18), the overflow pipe (12), riser (10 ), byproduct conversion reactor (11) the upper portion of the regenerator (18) is connected to the lower part of the methanol conversion reactor C3) connected to the regenerator (18) provided with an internal deaeration zone (20), the degassing zone (20) the catalyst through the overflow tube (1¾ conversion reactor into the by-product (11), by-product conversion reactor (11) the lower part of the outlet opening catalyst, with methanol conversion reactor via a catalyst feed pipe (5) (3) is connected, methanol conversion reactor (3) internally provided with a stripping zone (6), a stripping zone (6) through the catalyst riser (10) enters the regenerator (18), the methanol conversion reactor (3) and the by-product conversion reactor (11) opened the upper exports, regenerator (18) opened the top of the flue gas outlet.
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。 According to 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 reaction of claims - reproducing apparatus, wherein said product outlet and the flue gas before export are set gas-solid cyclone.
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 to claim - reproducing apparatus, characterized in that said deaeration 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 reaction of claims - reproducing apparatus, characterized in that the regenerator (18) controlled by a built-taking heat regeneration temperature.
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 to claim - reproducing apparatus, characterized in that the methanol conversion reactor C3) may be disposed external or internal temperature control of the reaction heat remover.
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 claim - reproducing apparatus, characterized in that said deaeration 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 reaction of claims - reproducing apparatus, wherein said byproduct conversion reactor (11) Products and methanol conversion reactor (3) products share a separate process.
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 to claim - reproducing apparatus, wherein said by-product carbon - carbon six four mixed hydrocarbon.
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 reactor - reproducing apparatus, wherein said mixed hydrocarbon four carbon content greater than 80% by mass of hydrocarbons, the olefin content greater than 60% by mass.
Descripción  traducido del chino

甲醇制低碳烯烃反应-再生装置 MTO reaction - reproducing apparatus

技术领域 Technical 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 reaction - reproducing apparatus. 技术背景 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] 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 petroleum resources to produce ethylene, propylene is 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. 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, 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 ester), etc. These can be converted from an oxygenate by coal, natural gas, biomass and other energy sources. 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 can already achieve large-scale production, such as methanol, can be obtained from coal or natural gas, technology is very mature, can achieve megaton scale of production. 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。 Due to extensive source of oxygen-containing compounds, transformed to produce light olefins plus economics of the process, so-to-olefin (OTO) from the oxygenate conversion process, in particular by the conversion of methanol to olefins (MTO) process more increasingly more attention.

[0003] US4499327专利中对磷酸硅铝分子筛催化剂应用于甲醇转化制烯烃工艺进行了详细研究,认为SAP0-34是MTO工艺的首选催化剂。 [0003] US4499327 patent phosphate aluminosilicate molecular sieve catalyst for converting methanol to olefins process were studied in detail that SAP0-34 is the preferred catalyst 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, allows the conversion of methanol to light olefins to the extent that the reaction time of less than 10 seconds, more even to the riser of the reaction time.

[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 oxide are converted to light olefins and reactor technology, the use of fast fluidized bed reactor, the gas velocity in the gas phase of the dense phase reaction zone lower the reaction was completed, up to the inner diameter of rapid change After small fast partition, using a special gas-solid separation equipment preliminary separating 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 prevent the occurrence of secondary reactions. 经模拟计算,与传统的鼓泡流化床反应器相比,该快速流化床反应器内径及催化剂所需藏量均大大减少。 After the simulation, compared with conventional bubbling fluidized bed reactor, the fast fluidized bed reactor volume required to hiding diameter and catalyst 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 reactor riser with a central oxide catalyst for the conversion of light olefins loop process, the apparatus comprises a set of a plurality of riser reactors, gas-solid separation zone, a plurality of offset components, etc., each riser reactor each having a catalyst injection port, bringing together to set up a separation zone, 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, and to ensure a high selectivity to light olefins, requires a certain amount of coke on the catalyst, and the conversion of methanol to olefins process of the reaction is very sensitive to temperature and other process parameters. 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 reaction zone coke catalyst, the reaction temperature fluctuations 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。 In addition, during the preparation of methanol to light olefins, inevitably will produce some byproducts such as carbon four or more hydrocarbons, etc. If 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。 The present invention is targeted to solve the above problems.

发明内容 DISCLOSURE

[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。 Technical Problem [0007] The present invention solves the yield of light olefins present in the prior art is not high, to provide a new MTO reaction - reproducing apparatus. 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 the production of 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 scheme is as follows: An MTO reaction - regeneration means, including methanol conversion reactor 3, byproduct conversion reactor 11, regenerator 18, the overflow pipe 12, riser 10, byproduct conversion reactor 11 is connected to the upper portion of the regenerator 18, the lower portion of the methanol conversion reactor 3 is connected to the regenerator 18 is provided inside the degassing region 20, 20 within the degassing zone through the overflow pipe 12 catalyst by-products into the conversion reactor 11, the lower portion 11 byproduct conversion catalyst reactor outlet opening, connected through a catalyst feed pipe 5 and the methanol conversion reactor 3, 3 is provided inside the methanol conversion reactor stripping zone 6, the stripping zone 6 the catalyst through the riser 10 into the regenerator 18, methanol conversion reactor 3 and byproduct conversion reactor 11 has opened the upper product outlet opening 18 at the top of the regenerator flue gas outlet.

[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] The above technical solution, the catalyst comprises a molecular sieve SAP0-34; the product prior to export and have set up a gas-solid cyclone flue gas outlet; the degassing zone 20 degassing medium is selected from water vapor, stripping District 6 stripping medium is selected from water vapor, the riser 10 to enhance the medium is selected from water vapor; the regenerator 18 through the built-in controls for heat regeneration temperature; the methanol conversion reactor 3 can be set to internal or external heat remover controlling the reaction temperature; the degassing zone 20 and an upper side wall stripping zone 6 is opened at least one catalyst inlet; the byproduct conversion reactor 11 and product methanol conversion reactor 3 products share a separation process; the sub- The product is a carbon - carbon six four mixed hydrocarbons; said hydrocarbon mixed hydrocarbon four carbon content greater than 80% by mass, the 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 will inevitably produce byproducts of four or more carbon hydrocarbons, byproducts this part of the production rate, and olefin content, the study found that this part of the high olefin content of carbon four above is a good mix of hydrocarbon raw material 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。 The method according to the present invention, setting a byproduct reformer, mainly for carbon byproducts six four - carbon hydrocarbon conversion of methanol to olefins formed during, for yield of light olefins. 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。 Byproduct reformer catalyst from the regenerator directly, will help to ensure the reaction temperature and catalyst activity four or more carbon hydrocarbon conversion required. 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 have found that more than four carbon hydrocarbon conversion will generate 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 converter by-products, the temperature decreased, a corresponding reduction in the methanol conversion reactor for heat load. 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 adopt the reactor, the regenerator is arranged in parallel, a larger floor space, longer catalyst transfer 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 used in the regenerator, byproduct reformer, the methanol conversion reactor arranged coaxially, greatly reducing the traditional response - footprint reproducing apparatus, while greatly reducing 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; the product prior to export and have set up a gas-solid cyclone flue gas outlet; the degassing zone 20 degassing medium is selected from water vapor, stripping zone 6 stripping medium is selected from water vapor, the riser 10 to enhance the medium is selected from water vapor; the regenerator 18 through the built-in controls for heat regeneration temperature; the methanol conversion reactor 3 may be provided externally or internally take controlling the temperature of the reaction heat; the degassing zone 20 and an upper side wall stripping zone 6 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 - carbon six four mixed hydrocarbon; the four mixed hydrocarbon carbon content greater than 80% by mass of hydrocarbons, the olefin content greater than 60% by mass, methanol conversion reactor outlet product yield of the carbon-based lower olefins 80. 67% (by weight), the conversion reactor byproduct exports light olefins yield reached 35.47% (by weight), and achieved good technical results.

附图说明 Brief Description

[0012] 图1为本发明所述方法的流程示意图。 [0012] FIG. 1 a schematic flow diagram 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。 [0013] FIG. 1, 1 is a feed medium to enhance the riser; stripping medium 2 is fed; 3 methanol conversion reactor; 4 raw feed is methanol; catalyst feed pipe 5; 6 to a stripping zone; 7 is a side wall catalyst inlet stripping zone; 8 outside the reactor heat remover; 9 gas-solid cyclones; 10 for the riser; 11 conversion reactor byproducts; 12 is the overflow tube; 13 for the gas-solid cyclones; 14 byproduct feed; 15 exports; 16 to the plenum; 17 for the regeneration medium feed; regenerator 18; 19 degassing medium feed; 20 for the degassing zone; 21 regenerative heat remover; 22 gas-solid cyclones; 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] raw material feed line 4 into the methanol conversion reactor 3, the contact with a molecular sieve catalyst, the reaction product containing light olefins, after rapid gas-solid separation device 9 into the plenum chamber 16 separated, deactivated catalyst after After stripping stripping zone 6 via the riser 10 into the regenerator 18 regenerated, the regenerated catalyst through the overflow pipe 12 into the by-product in the conversion reactor 11, in contact with four or more carbon byproduct hydrocarbon, the resulting product through a gas-solid cyclone After separation of the separator into the plenum 13, by-products of the reforming catalyst in the reactor through a catalyst feed pipe 5 into the methanol conversion reactor 3, the reaction was continued with methanol.

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

具体实施方式 DETAILED DESCRIPTION

[0016]【实施例1】 [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, but is not set plenum, the methanol conversion reactor product and by-product into separate 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 is 170 kg / cubic meter, the average temperature conversion reactor byproduct was 552 ° C, the bed density was 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。 Reaction - atmospheric pressure regeneration system, methanol conversion reactor purity of 99.5% of the methanol feed, the feed was 1 kg / h, the catalyst is SAP0-34, stripping medium stripping zone, the degassing zone off gas medium riser enhance media are water vapor, taking heat regenerator temperature setting coil 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 four or more carbon mixed hydrocarbon, wherein four hydrocarbon carbon content of 91% by mass, the olefin content of 87% by mass, the amount of the regenerated catalyst was 0.47% carbon, from the conversion reactor byproduct out The amount of carbon catalyst was 1.6%, maintaining the stability of the catalyst flow control products are used in the reactor outlet line gas chromatographic analysis of methanol conversion reactor outlet carbon-based products, light olefins yield 80.67% (by weight), Deputy product conversion reactor outlet 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] according to the conditions described in Example 1, the byproduct conversion reactor feed four or more carbon mixed hydrocarbon, wherein the hydrocarbon of four carbon content of 80% by mass, the olefin content of 60% by mass, the amount of regenerated catalyst coke 0 . 27%, the amount of catalyst from the coke by-products out of the conversion reactor is 1.18%, the flow of control to maintain stability of the catalyst, the reactor outlet products were analyzed using online gas chromatography, the methanol conversion reactor outlet product Low carbon-based olefins yield 80.48% (by weight), the conversion reactor byproduct exports light 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] The embodiment according to the conditions described in Example 1, no byproduct conversion reactor, regenerated catalyst is returned directly to the lower portion of the methanol conversion reactor, the carbon-based olefins yield 79.63% by weight.

[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 is a method that can achieve the purpose of improving the yield of light olefins, with great technical advantages, can be used in the industrial production of light olefins.

Citas de patentes
Patente citada Fecha de presentación Fecha de publicación Solicitante Título
CN1962573A *1 Dic 200616 May 2007中国化学工程集团公司Method and reactor for catalytic cracking for producing propylene using fluid bed
CN101402538A *21 Nov 20088 Abr 2009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
US6166282 *20 Ago 199926 Dic 2000Uop LlcFast-fluidized bed reactor for MTO process
Citada por
Patente citante Fecha de presentación Fecha de publicación Solicitante Título
CN102872770A *12 Jul 201116 Ene 2013中国石油化工股份有限公司Reaction unit for preparing low-carbon olefins
CN102872770B *12 Jul 20118 Abr 2015中国石油化工股份有限公司Reaction unit for preparing low-carbon olefins
CN103537235A *12 Jul 201229 Ene 2014中国石油化工股份有限公司Reaction device for preparing low-carbon olefin by using oxy-compounds
CN103537235B *12 Jul 201213 Abr 2016中国石油化工股份有限公司含氧化合物制低碳烯烃的反应装置
Clasificaciones
Clasificación internacionalC07C11/04, C07C1/20, C07C4/06, C07C11/06
Clasificación cooperativaY02P20/52, Y02P30/42, Y02P20/584
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14 Dic 2011C06Publication
1 Feb 2012C10Entry into substantive examination
28 May 2014C14Grant of patent or utility model