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Número de publicaciónCN102020523 B
Tipo de publicaciónConcesión
Número de solicitudCN 200910170274
Fecha de publicación5 Jun 2013
Fecha de presentación10 Sep 2009
Fecha de prioridad10 Sep 2009
También publicado comoCN102020523A
Número de publicación200910170274.4, CN 102020523 B, CN 102020523B, CN 200910170274, CN-B-102020523, CN102020523 B, CN102020523B, CN200910170274, CN200910170274.4
Inventores余龙红, 王子宗, 吴雷, 杨德祥
Solicitante中国石油化工股份有限公司, 中国石化工程建设有限公司
Exportar citaBiBTeX, EndNote, RefMan
Enlaces externos:  SIPO, Espacenet
Operating method for olefin conversion device
CN 102020523 B
Resumen  traducido del chino
本发明属于一种烯烃转化装置的开工方法,涉及甲醇、二甲醚等有机氧化物制取烯烃,如MTO、MTP的装置,其特征在于该装置开工时,反应器2、再生器3的催化剂分别从各自的催化剂罐引入,分两路加剂,两器各自加入的催化剂升温依靠单独设置的外界热源和加热媒介,即反应器2设置开工蒸汽过热器1,以高温蒸汽加热催化剂;再生器3设置辅助燃烧室,以高温空气加热催化剂。 The present invention pertains to a method of operating an olefin conversion means, methanol, dimethyl ether and other organic oxides preparing olefins such as MTO, MTP device relates, characterized in that when the device starts, the catalyst reactor 2, the regenerator 3 cans from their respective catalyst introduced two routes additives, each added two devices rely on external sources of heat and a catalyst temperature heating media set individually, that reactor 2 is set to start a steam superheater, steam heated to a high temperature catalyst; regenerator 3 Set the secondary combustion chamber, the air is heated to a high temperature catalyst. 在加剂时,不由再生器3向反应器2转剂,两器之间无催化剂输送。 When the additive, the reigning 3 2 transfer agent regenerator to the reactor, no catalyst transfer between two devices.
Reclamaciones(5)  traducido del chino
1.一种烯烃转化装置的开工方法,包括向反应器(2)、再生器(3)中加入催化剂、催化剂的预热以及催化剂在反应器(2)和再生器(3)之间的转移,其特征在于: 反应器(2)、再生器(3)催化剂分别从各自的催化剂罐引入、分两路加剂; 在加剂时,不由再生器(3)向反应器(2)转剂,两器之间无催化剂输送; 所述的反应器(2)设置开工蒸汽过热器(I),以高温蒸汽加热催化剂,所述的反应器(2)引入的过热蒸汽作为外界热源和加热媒介; 所述的再生器(3)设置辅助燃烧室(4),以高温空气加热催化剂; 所述高温蒸汽的温度为400°C至500°C,所述高温空气的温度为700°C至750°C ; 开工加剂时,在斜管上滑阀未打开之前,反应系统的待生斜管、反应外取热下斜管中催化剂未循环流动,斜管松动介质采用非蒸汽; 所述的烯烃转化装置,其中包括甲醇制烯烃装置。 1. A method of operating an olefin conversion apparatus, comprising the reactor (2), the regenerator (3) catalyst was added, and the catalyst warm-transfer catalyst in the reactor (2) and a regenerator (3) between the characterized in that: the reactor (2), the regenerator (3) the catalyst are introduced from the respective catalyst containers, two routes additives; at PPD, not by the regenerator (3) to the reactor (2) transfer agent , no catalyst is conveyed between the two; the reactor (2) is provided to start the steam superheater (I), to a high temperature steam heating the catalyst, said reactor (2) the introduction of superheated steam as the heating medium and the external heat source ; regenerator (3), wherein an auxiliary combustion chamber (4), the catalyst was heated to a high temperature air; the temperature of the high temperature steam is 400 ° C to 500 ° C, the temperature of the hot air is 700 ° C to 750 ° C; when started before additives on chute slide valve does not open, student response system to be inclined tube, outside of the reaction to take the heat down tube is not the catalyst circulation, loosen the media using non-inclined tube steam; said olefins conversion unit, including methanol to olefins unit.
2.如权利要求1的烯烃转化装置的开工方法,其特征在于: 所述的开工蒸汽过热器(I)将蒸汽温度过热至400-500°C后,注入反应器(2)直接加热加入反应器(2)的催化剂,使其温度升至350°C以上。 2. The operating method of olefin conversion device according to claim 1, wherein: said operating steam superheater (I) the temperature of the steam superheated to 400-500 ° C and then charged into the reactor (2) is directly heated to the reaction (2) a catalyst, its temperature was raised to 350 ° C or more.
3.如权利要求1的烯烃转化装置的开工方法,其特征在于: 所述的辅助燃烧室(4)的加热空气使再生器(3)的催化剂升温高于300-350°C、并且再生器(3)内催化剂料位达到淹没燃烧油喷嘴时,再生器(3)喷入燃烧油,依靠燃烧油加热催化剂,升温与加剂速度均加快;或全程采用辅助燃烧室(4)将再生器的催化剂加热至550°C以上。 3. The operating method of olefin conversion device according to claim 1, wherein: the auxiliary combustion chamber (4) of the heated air to the regenerator (3) of the catalyst temperature rise above 300-350 ° C, and the regenerator (3) within the catalyst material level reaches the submerged combustion of oil nozzle, regenerator (3) is injected into the combustion of oil, relying on heating oil combustion catalyst, temperature and speed are additive to accelerate; or full use of the secondary combustion chamber (4) the regenerator The catalyst was heated to 550 ° C and above.
4.如权利要求2或3所述的烯烃转化装置的开工方法,其特征在于: 装剂结束时,反应器(2)温度不低于350°C、再生器(3)温度不低于550°C,并且两器均达到0-50kPa,料位50-65%后,打开再生、待生滑阀,依靠自身的压力平衡,达到两器之间的催化剂循环;此时,斜管松动介质切换成装置正常运行的松动介质。 4. The operating method of olefin conversion apparatus according to claim 2 or claim 3, characterized in that: the end of the loading agent, the reactor (2) temperature of not lower than 350 ° C, the regenerator (3) temperature of not less than 550 ° C, and the two devices are up 0-50kPa, 50-65% after the material level, open regeneration, spent slide valve, the pressure on their own balance, reach catalyst circulation between the two; this time, the inclined tube loose medium loosen the media device is switched to normal operation.
5.如权利要求1所述的烯烃转化装置的开工方法,其特征在于: 所述的烯烃转化装置包括甲醇制丙烯装置。 5. A method of operating an olefin conversion apparatus according to claim 1, characterized in that: the olefin conversion means comprises means methanol to propylene.
Descripción  traducido del chino

一种烯烃转化装置的开工方法 Start of olefins conversion unit of

技术领域 FIELD

[0001] 本发明属于一种烯烃转化装置的开工方法,涉及甲醇、二甲醚等有机氧化物制取烯烃(如ΜΤ0、ΜΤΡ)的装置。 [0001] The present invention pertains to a method of operating an olefin conversion apparatus involving methanol, dimethyl ether and other organic oxides Preparation olefins (e.g. ΜΤ0, ΜΤΡ) apparatus.

背景技术 BACKGROUND

[0002] 轻烯烃在这里定义为乙烯、丙烯、丁烯及其混合物,是生产多种重要的化学品和聚合物的原料。 [0002] Light olefins is defined herein as ethylene, propylene, butylene and mixtures thereof, is the production of a variety of important chemical and polymer materials. 轻烯烃典型地是通过石油原料裂解生产的,由于竞争性石油原料的有限供给,并且国际价格日趋高涨,从石油原料生产轻烯烃显得越来越不经济,生产成本也增加较快,为此,基于替代原料生产轻烯烃技术的开发显得日益迫切,并发挥越来越重要的作用。 Light olefins are typically produced by the cracking of petroleum feedstock, due to the limited supply of competitive petroleum feedstocks, and increasingly high international prices, the production of light olefins from petroleum feedstocks become increasingly uneconomic production costs also increased rapidly, therefore, alternative raw materials to produce light olefins technology-based development is becoming increasingly urgent, and play an increasingly important role.

[0003] 用于生产轻烯烃的重要替代原料是含氧化合物,如醇,尤其是甲醇和乙醇,二甲醚、甲乙醚、二乙醚、碳酸二甲酯和甲酸甲酯等。 Important alternative raw materials [0003] for the production of light olefins are oxygenates, such as alcohols, especially methanol and ethanol, dimethyl ether, methyl ethyl ether, diethyl ether, dimethyl carbonate and methyl formate and the like. 这些含氧化合物很多种可以通过发酵来生产,或者衍生自生物质原料、天然气、石油液体,还包括由煤、回收塑料、城市废弃物或含有任何有机材料等在内的含碳材料的合成气来生产。 These oxygenates may be produced by a wide variety of fermentation, or is derived from biomass feedstock, natural gas, petroleum liquids, further comprising from coal, recycled plastics, municipal wastes, or any organic material containing such, including the carbonaceous material to synthesis gas produce. 由于来源广泛,醇、醇衍生物和其它含氧化合物等非石油原料作为烯烃生产,具有广阔的经济前景。 Due to wide variety of sources, non-petroleum alcohol, alcohol derivatives, and other oxygenates, such as as the olefin production, with vast economic prospects.

[0004] 含氧化合物烯烃转化工艺是以含氧化合物为原料,与专门的硅铝磷酸盐(SAPO)分子筛催化剂相接触,应用流化技术,在合适的反应工艺条件下,包括温度、压力、床层空速及其表观线速、催化剂积碳量、反应(停留)时间及实施各因素相互之间的控制方法等,发生转化反应,以制取低碳烯烃等的工艺方法。 [0004] The oxygenate conversion process is based on oxygen-containing olefin compound as a raw material, and special silicoaluminophosphate (SAPO) molecular sieve catalyst is contacted, application streaming technology, under suitable reaction conditions, including temperature, pressure, bed airspeed and the apparent line speed, the amount of carbon catalyst, the reaction (dwell) time and the implementation of various factors, such as mutual control method, the occurrence of conversion reaction to produce light olefins such as taking process method. 与成熟的催化裂化工艺相类似,转化反应和催化剂烧焦再生连续进行,反应器不断补充再生后的催化剂,维持催化剂活性和产品选择性稳定,使转化反应平稳进行。 Similar to the mature phase catalytic cracking process, the conversion reaction and catalyst regeneration burning continuously, the reactor after the catalyst regeneration constantly replenished to maintain a stable catalyst activity and product selectivity, so that the conversion reaction proceed smoothly.

[0005] 现有催化裂化装置开工过程是: [0005] existing FCCU operating process is:

[0006] I)反应器、再生器系统内的催化剂均从再生器加入,在加剂初期,依靠辅助燃烧室加热空气来使加入的催化剂升温,辅助燃烧室加热空气的最高温度一般不超过780°C ;当再生器内初装的催化剂料位达到淹没燃烧油喷嘴时,并且温度高于300-350°C时,喷入燃烧油,依靠燃烧油加热催化剂,升温速度加快。 [0006] I) of the reactor, a catalyst regenerator in the system from the regenerator are added, at the beginning of additives, relying on the auxiliary combustion chamber so that the heated air is added to the catalyst to heat up, the auxiliary combustion chamber maximum temperature of the heated air is generally not more than 780 ° C; when the catalyst regenerator material level reaches the initial installation of submerged oil burner nozzles, and temperatures above 300-350 ° C, is injected into the combustion of oil, relying on heating oil combustion catalyst, heating speed.

[0007] 2)当再生器内催化剂装至一定料位,温度达到500°C以上时,向反应器转剂。 [0007] 2) When the catalyst regenerator filled to a certain material level, the temperature reached 500 ° C above the reactor transfer agent.

[0008] 3)第一次转剂完成后,关闭滑阀,再生器继续加剂,升温。 [0008] 3) after the first transfer agent is complete, close the slide valve, regeneration continues additives, heat up.

[0009] 4)当再生器催化剂料位、温度达到指标后,打开滑阀,进行第二次转剂。 [0009] 4) When the regenerator catalyst material level, short of the target temperature, open the slide valve, a second transfer agent. 由于再生器空间比反应器空间大很多,只需要一、二次转剂,就能建立再生器-反应器之间的催化剂循环。 Since the regenerator space much larger than the reactor space, only one, the secondary transfer agent, will be able to establish the regenerator - catalyst recycle between the reactors. 两次转剂的时间间隔应尽量短,因为转入反应器的热催化剂依靠蒸汽流化,温度在慢慢降低,不能引起催化剂“和泥”。 The time interval between two transfer agent should be as short as possible, because the hot catalyst into the reactor, steam fluidized rely on the temperature slowly decreases, can not cause catalyst "and mud."

[0010] 5)任何装置的开工过程都是相对的不稳定过程,会引起系统催化剂的跑损,因此,这个过程进行得越快越好。 [0010] 5) to start the process of any device is relatively unstable process, will cause the system to run the catalyst loss, therefore, this process was carried out as quickly as possible. 一般的,对于催化裂化装置,装置自加剂开始至达到进料条件(即催化剂料位和温度达到指标要求),需要4-8小时即可完成。 In general, for fluid catalytic cracking unit, the device since the beginning of additives to achieve the feed conditions (ie catalyst material level and temperature specification requirements), take 4-8 hours to complete. 与重质油品催化裂化装置不同,在烯烃转化装置中,含氧化合物烯烃转化产品气除了乙烯、丙烯等低碳烯烃外,还副产大量的水和少量的C4及有机氧化物,其中乙烯、丙烯约占23v %,水占72v %,气体量大,气体产品平均分子量小,产品气的体积流量大;相应地,对于再生器系统,I)氧化物烯烃转化生焦率低,只有重质油品催化裂化的1/3-1/4 ;2)转化反应要求再生催化剂需含有l-2wt%的定碳,再生烟气含有CO,耗风指标低,因此,总再生烟气量小。 With the heavy oil FCCU is different in olefin conversion apparatus, the oxygenate conversion of the olefin product gas in addition to ethylene, propylene and other olefins, but also a large amount of by-product water and a small amount of C4 and organic oxides, wherein the ethylene , propylene accounting 23v%, water accounts 72v%, gas volume, gas product average molecular weight is small, a large volume flow of product gas; Accordingly, for the regenerator system, I) oxide olefin conversion low coke, only heavy quality oil catalytic cracking 1 / 3-1 / 4; 2) conversion reactions require regeneration of the catalyst need contain l-2wt% of Dingtan, regenerated flue gas comprising CO, low air consumption indices, therefore, a small amount of the total regeneration flue gas . 举例来说,180万吨/年甲醇制烯烃(MTO)装置,反应器在0.20-0.40MPa(a)、450_550°C的反应条件下,出反应器的产品气体积流量为64.297m3/s ;再生器0.15MPa(g),680°C的条件下,出再生器烟气体积流量为23.llm3/s,反应器产品气量接近于3倍的再生烟气量,因此,烯烃转化反应决定了大反应、小再生,反应器远比再生器大。 For example, 1.8 million tons / year of methanol to olefins (MTO) unit reactor under reaction conditions 0.20-0.40MPa (a), 450_550 ° C, and the reactor product gas volume flow of 64.297m3 / s; Under the regenerator 0.15MPa (g), 680 ° C condition, the regenerator flue gas volume flow 23.llm3 / s, the reactor product gas close to 3 times the amount of regenerated flue gas, therefore, determines the olefin conversion reaction Large reaction, a small regeneration, the reactor than the regenerator large. 而对于催化裂化装置,再生烟气体积流量是反应油气体积流量的2.4倍,再生器远比反应器大。 For catalytic cracking unit, regenerated flue gas volume flow rate and gas volume flow rate of the reaction is 2.4 times, than the reactor regenerator large. [0011] 综上所述,由于烯烃转化装置与重油催化裂化装置有如下不同的工艺特点,因而需要采取不同的开工方法:[0012] I)两器体积相差悬殊,反应器远大于再生器,与催化裂化装置完全相反;[0013] 2)生焦量少,决定了烯烃转化装置的再生系统,包括再生器、主风机、辅助燃烧室等相配套的设备均较小,大大降低了开工加剂与升温速度。 [0011] In summary, the olefins conversion unit and FCCU has the following characteristics of different processes, which require different operating methods: [0012] I) volume differences between the two devices, the reactor is much larger than the regenerator, and FCCU exact opposite; [0013] 2) less coke determines regeneration system olefins conversion unit, including the regenerator, the main fan, auxiliary combustion chamber and other supporting devices are small, greatly reducing start plus agent and the heating rate. [0014] 3)正常操作时,转化反应两器之间的催化剂循环量小,设置的斜管与滑阀也较小,满足不了开工时如同催化裂化装置开工通过再生器向反应器转剂的要求。 When the [0014] 3) normal operation, a small conversion reaction catalyst circulation between the two inclined pipe and slide valve set is smaller, met not start operating as FCCU regenerator to the reactor through the transfer agent Claim. [0015] CN 1836027A公开了一种起动反应系统的方法,该反应系统是使用包含分子筛,尤其金属铝磷酸盐分子筛,尤其容易由于与水分子接触而损失催化活性的金属铝磷酸盐分子筛的催化剂的那些系统。 [0015] CN 1836027A discloses a method of starting the reaction system, the reaction system containing a molecular sieve, in particular metal aluminophosphate molecular sieve, particularly vulnerable due to loss of contact with water molecules and the catalytic activity of metal aluminophosphate molecular sieve Those systems. 该方法提供了加热和装载活化分子筛以防止能够由于与水分子接触而发生的催化剂活性损失的适当手段。 This method provides the heating and loading activated molecular sieves suitable means to prevent contact with water molecules can be caused to occur catalyst activity loss. [0016] CN 101130466A公开了一种由甲醇或/和二甲醚制取低碳烯烃的流态化反应装置的开工方法,包括利用开工辅助热源将循环流态化催化反应装置的催化剂床层加热到200°C或300°C以上后向反应器输送甲醇或二甲醚原料,反应放热使反应系统装置快速升温至指定温度,从而使系统迅速达到正常运行状态。 [0016] CN 101130466A discloses a method for operating a take from methanol or / and dimethyl ether to olefins in fluidized reaction apparatus, including the use of an auxiliary heat source would start circulating fluidized catalyst bed catalytic reaction device of heating to 200 ° C or 300 ° C or more after delivery methanol or dimethyl ether raw materials to the reactor, the reaction system means the exothermic reaction quickly warmed to a specified temperature, so that the system can be quickly reached normal operating state. 此方法适用于放热型流态化催化反应装置的开工过程,能够简化设备和操作,节省成本。 This method applies to start the process of fluidized catalytic exothermic reaction device that simplifies equipment and operating cost savings. [0017] CN 1836027A提供了了加热和装载活化分子筛以防止能够由于与水分子接触而发生的催化剂活性损失的适当手段,催化剂与水分子接触使催化剂失活是在600°C以上的高温下发生的,在较低的温度下不易使催化剂失活;CN 101130466A是温度上升至200°C或300°C以上后,向反应器输送甲醇或二甲醚原料,借助于反应放热使反应系统装置快速升温的方法,由于反应系统催化剂藏量大,以开工辅助热源将两器系统的催化剂床层加热到200°C或300°C以上也需耗费较长的时间,而且此时再生系统也维持此温度,而使烧焦无法进行。 [0017] CN 1836027A provides a heat activated molecular sieves and load the appropriate means able to prevent contact with water molecules due to the occurrence of loss of catalyst activity, with water molecules contacting catalyst deactivating the catalyst occurs at temperatures above 600 ° C and at lower temperatures easily deactivate the catalyst; CN 101130466A the temperature is increased to 200 ° C or above 300 ° C, the reactor is conveyed to the methanol or dimethyl ether raw materials, the reaction system by means of an exothermic reaction means rapid heating method, since the reaction system catalyst inventory amount, to start the two auxiliary heat source system of the catalyst bed was heated to 200 ° C or above 300 ° C also need to spend a long time, but this time the regeneration system is also maintained this temperature, leaving charred impossible. 发明内容[0018] 本发明的目的在于提供一种烯烃转化装置的开工方法,反应器、再生器分两路各自加剂、升温,不由再生器向反应器转剂,两器之间无催化剂输送。 SUMMARY OF THE INVENTION [0018] The object of the present invention to provide a method of operating an olefin conversion apparatus, a reactor, a regenerator two routes each additive, heating, not help the regenerator to the reactor transfer agent, no catalyst transport between two devices . [0019] 本发明的烯烃转化装置的开工方法是这样实现的:[0020] 本发明的烯烃转化装置的开工方法,包括向反应器2、再生器3中加入催化剂、催化剂的预热以及催化剂在反应器2和再生器3之间的转移,其特征在于:[0021] 反应器2、再生器3催化剂分别从各自的催化剂罐引入、分两路加剂;[0022] 在加剂时,不由再生器3向反应器2转剂,两器之间无催化剂输送。 [0019] The method starts olefin conversion apparatus of the present invention is implemented as follows: [0020] The method starts olefin conversion apparatus of the present invention, including 2, the regenerator 3 catalyst was added to the reactor, the preheating of the catalyst and the catalyst in 3 transfer between reactor and regenerator 2, wherein: [0021] The reactor 2, a catalyst regenerator 3 from the respective catalyst containers are introduced, two routes additives; [0022] In the additive, the help regenerator transfer agent to the reactor 2, the catalyst-free between the two conveyor 3.

[0023] 在具体实施中, [0023] In a specific embodiment,

[0024] 所述的反应器2、再生器3加入的催化剂升温依靠各自单独设置的外界热源和加热媒介; [0024] The reactor 2, the regenerator 3 catalyst was added and heating rely on external heat source of the heating medium are each separately provided;

[0025] 所述的反应器2设置开工蒸汽过热器1,以高温蒸汽加热催化剂; [0025] The reactor 2 is provided to start a steam superheater 1, high temperature steam heating the catalyst;

[0026] 所述的再生器3设置辅助燃烧室4,以高温空气加热催化剂; Regenerator [0026] 3, wherein the auxiliary chamber 4, the air is heated to a high temperature catalyst;

[0027] 所述的开工蒸汽过热器I将蒸汽温度过热至400-50(TC后,注入反应器2直接加热加入反应器2的催化剂,使其温度升至350°C以上; Start steam superheater [0027] The temperature of the steam superheated to I 400-50 (after TC, injected into the reactor 2 was added directly heating the catalyst reactor 2, so that the temperature was raised to 350 ° C or more;

[0028] 其中,过热蒸汽一方面为催化剂升温提供热量;另一方面作为流化介质,赶走反应器2内的空气。 [0028] wherein the superheated steam to provide heat for the catalyst temperature raising one hand; on the other hand as a fluidized medium, off the air inside the reactor 2.

[0029] 在加剂初期,所述的辅助燃烧室4的加热空气使再生器3的催化剂升温高于300-35(TC、并且再生器3内催化剂料位达到淹没燃烧油喷嘴时,再生器3喷入燃烧油,依靠燃烧油加热催化剂,升温与加剂速度均加快;或全程采用辅助燃烧室4将再生器的催化剂加热至550°C以上;辅助燃烧室只加热加至再生器3内的催化剂,并使其升温。 [0029] In the early additives, said auxiliary chamber heated air 4 3 catalyst regenerator temperature higher than 300-35 (TC, and three in the catalyst regenerator material level reaches the submerged combustion of oil nozzle, regenerator 3 is injected into the combustion of oil, heating oil combustion catalyst rely, heating rate and additives are accelerated; or full use of the secondary combustion chamber catalyst regenerator 4 heated to 550 ° C or more; auxiliary combustion heating only added to the regenerator 3 within catalyst, and allowed to warm.

[0030] 所述的反应器2引入的过热蒸汽温度、流量等需满足流化表观线速度和升温、力口剂速度的要求。 Reactor [0030] 2 introduced the superheated steam temperature, flow, etc. need to meet the flow of superficial linear velocity and temperature, force mouth agent speed.

[0031] 开工加剂时,在斜管上滑阀未打开之前,反应系统的待生斜管、反应外取热下斜管等催化剂未循环流动,斜管松动(注:为了维持稳定的催化剂流化和输送,在斜管上每隔一定距离引入外来气体,如蒸汽、氮气、空气等,以松动催化剂,防止架桥。)介质采用非蒸汽。 Prior to the time [0031] started additives on chute slide valve does not open until the birth of the reaction system inclined tube, outside of the reaction tubes for heat ramp catalyst does not circulate, inclined tube loose (Note: In order to maintain the stability of the catalyst fluidizing and transport, at regular intervals from the introduction of foreign gases, such as steam, nitrogen, air or the like in the inclined tube to loosen the catalyst, to prevent bridging.) non-vapor medium.

[0032] 装剂结束时,反应器2温度不低于350°C、再生器3温度不低于550°C,并且两器均达到所需要的料位0-50kPa,50-65%后,打开再生、待生滑阀,依靠自身的压力平衡,达到两器之间的催化剂循环;此时,斜管松动切换成装置正常运行所采用的松动介质。 [0032] At the end of loading agent, the reaction temperature is not lower than 2 350 ° C, the regenerator temperature is not lower than 3 550 ° C, and the two devices are expected to achieve the required bit 0-50kPa, 50-65%, Open regeneration, spent slide valve, the pressure on their own balance, reach catalyst circulation between the two; this time, the inclined tube loose switch to loosen the media device used in normal operation.

[0033] 所述的烯烃转化装置,其中包括甲醇制烯烃(MTO)装置和甲醇制丙烯(MTP)装置。 [0033] The olefins conversion unit, including the methanol to olefins (MTO) unit and methanol to propylene (MTP) device.

[0034] 本发明的效果是: [0034] The effect of the present invention are:

[0035] I本发明因反应器2、再生器3加剂量不同,加入的催化剂终温不同,因此,加剂速度、升温速度不同,分开加剂和升温,有利于灵活控制,时间上达到一致。 [0035] I the present invention due to the reactor 2, the regenerator 3 different dosage, different final temperature was added catalyst, therefore, additive speed, different heat-up rate additive and separate heating conducive flexible control, the time to reach consensus .

[0036] 2本发明催化剂升温由于采用两个不同热源提供,因此升温速度快。 Catalyst [0036] 2 heating due to the use of two different invention provides a heat source, so fast heating rate.

[0037] 3由上述1、2的原因,本发明缩短开工时间,避免多次转剂;并且避免了由其造成的反应器2催化剂因温度降低而“和泥”,从而堵塞待生斜管;同时,也减少开工过程中反应器2、再生器3催化剂的跑损。 [0037] 1, 2, 3 by the above reasons, the present invention is to shorten the starting time, to avoid repeated transfer agent; and avoids reactor 2 by the catalyst temperature decrease caused by "mud", thereby clogging the spent inclined tube ; while also reducing reactor 2 starts the process, the catalyst regenerator 3 run loss.

[0038] 4开工过程中反应器、再生器各自装剂时,斜管上滑阀未打开、两器催化剂未循环流动,斜管松动采用非蒸汽介质,如不会冷凝的空气、氮气等,避免了斜管堵塞。 [0038] 4 to start the process reactor, regenerator means when the respective agents, the inclined tube slide valve is not open, the two catalysts is not circulating, loose non-inclined tube steam medium, such as air does not condense, such as nitrogen, Avoid the inclined tube blockage.

附图说明 Brief Description

[0039] 下面结合附图对本发明作进一步详细描述: [0039] OF THE DRAWINGS The present invention will be described in detail:

[0040] 图1 一种烯烃转化装置的开工方法的示意图 The method of operating a schematic view [0040] FIG 1 An olefin conversion apparatus

[0041] 图中:1、开工蒸汽过热器;2、反应器;3、再生器;4、辅助燃烧室;5、反应器2催化剂罐5 ;6、再生器3催化剂罐6; [0041] Fig: 1, operating the steam superheater; 2, reactor; 3, regenerator; 4, an auxiliary combustion chamber; 5, the second catalytic reactor tank 5; 6, regenerator catalyst 3 tank 6;

[0042] 11、蒸汽11 ;12、过热蒸汽12 ;13、甲醇或二甲醚进料13 ;14、反应产品气14 ;15、反应器2催化剂加剂15 ; 16、反应器2催化剂卸剂16 ;21、空气21 ;22、高温空气22 ;23、再生烟气23 ;24、再生器3催化剂加剂24 ;25、再生器3催化剂卸剂25 ;31、待生催化剂31 ;32、再生催化剂33具体实施方式[0043] 开工时,蒸汽11经过开工蒸汽过热器11加热至400-50(TC后,变成过热蒸汽12,注入到反应器2,同时,自反应器2催化剂罐5加入常温的反应器2催化剂15,常温的反应器2催化剂15与过热蒸汽12在反应器2内充分混合,加热反应器2催化剂,并使之升温,为了控制升温速度,过热蒸汽量与加剂速度按一定的比例关系,并且随着反应器2加剂和温升的进行,需要做相应地调整。同时,对于再生器3系统,空气21经过辅助燃烧室4加热至700-750°C后,变成高温空气22,注入到再生器3,同时,自再生器3催化剂罐6加入常温的再生器催化剂24,常温的再生器催化剂24与高温空气22在再生器3内充分混合,加热再生器催化剂,并使之升温。在反应器2和再生器各自加剂、升温的同时,两器之间的待生催化剂31和再生催化剂32不循环,其滑阀是微开的,只有待反应器2、再生器3均加够催化剂和达到各自的终温反应器不低于350°C、再生器不低于550°C时,才打开滑阀,投用自动控制,使得两器之间催化剂进行循环、输送,循环正常后,两器各自的料位自动控制稳定后,投用甲醇或二甲醚进料13。在装置停工时,打开反应器2催化剂卸剂16和再生器催化剂卸剂25分别向反应器2催化剂罐5、再生器催化剂罐6卸剂。 [0042] 11, steam 11; 12, superheated steam 12; 13, methanol or dimethyl ether feed 13; 14, the reaction product gas 14; 15, 15 additive catalyst reactor 2; 16, the second catalytic reactor unloading agent 16; 21, air 21; 22, hot air 22; 23, 23 smoke regeneration; 24, 3 catalyst regenerator additives 24; 25, 3 catalyst regenerator unloading agent 25; 31, spent catalyst 31; 32, regeneration catalyst 33 DETAILED DESCRIPTION [0043] When started, the steam 11 through a steam superheater 11 starts heated to 400-50 (after TC, becomes superheated steam 12, injected into the reactor 2, while the second catalyst from the reactor tank 5 was added The catalyst reactor 2 at room temperature 15, the second catalytic reactor at room temperature 15 12 mixed with superheated steam in the reactor 2, the second catalytic reactor is heated and allowed to heat up, in order to control the rate of temperature increase, the amount of superheated steam and additive velocity according to a certain ratio between, and with two additives and temperature of the reaction, you need to be adjusted accordingly. At the same time, for the regenerator 3 system via the auxiliary combustion air 21 4 heated to 700-750 ° C, 22 becomes high temperature air, is injected into the regenerator 3, the same time, since the catalyst regenerator 3 tank 6 at room temperature was added a catalyst regenerator 24, the normal temperature of the catalyst regenerator 24 and the high-temperature air 22 mixed in the regenerator 3 within the heated regenerator catalysts, and make it to heat up. In the reactor and regenerator 2 each additive, heating, while two spent catalyst between 31 and 32 are not regenerated catalyst circulation, its slide valve is slightly open, only to be reactor 2, 3 are regenerated catalyst and add enough time to reach their final temperature of the reactor is not lower than 350 ° C, regeneration is not less than 550 ° C, and then opened the slide valve, cast with automatic control, so that the catalyst between the two devices After circulation and transportation, the normal cycle, the two devices after the respective material level automatic control is stable, and put into use methanol or dimethyl ether feed 13. In apparatus shutdown, the reactor was unloaded agent 16 and the second catalyst regenerator catalyst unloading agent 25 are a second catalyst to the reactor tank 5, the regenerator catalyst containers 6 unloading agent.

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Clasificaciones
Clasificación internacionalB01J38/12, C07C11/06, C07C11/02, C07C1/20
Clasificación cooperativaY02P20/584
Eventos legales
FechaCódigoEventoDescripción
20 Abr 2011C06Publication
8 Jun 2011C10Request of examination as to substance
25 Jul 2012C53Change or modification
5 Jun 2013C14Granted