CN102453506A - Hydrocarbon oil conversion method - Google Patents

Hydrocarbon oil conversion method Download PDF

Info

Publication number
CN102453506A
CN102453506A CN 201010518936 CN201010518936A CN102453506A CN 102453506 A CN102453506 A CN 102453506A CN 201010518936 CN201010518936 CN 201010518936 CN 201010518936 A CN201010518936 A CN 201010518936A CN 102453506 A CN102453506 A CN 102453506A
Authority
CN
Grant status
Application
Patent type
Prior art keywords
catalyst
regenerated catalyst
diesel
oil
reaction zone
Prior art date
Application number
CN 201010518936
Other languages
Chinese (zh)
Inventor
侯典国
张久顺
汪燮卿
谢朝钢
Original Assignee
中国石油化工股份有限公司
中国石油化工股份有限公司石油化工科学研究院
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date

Links

Abstract

The present invention provides a hydrocarbon oil conversion method. According to the method, a lift pipe reactor including an upper part reaction zone and a lower part reaction zone is adopted; a diesel raw material, a regeneration catalyst and/or a semi-regeneration catalyst are introduced to the lower part reaction zone, such that the diesel raw material and the catalyst are subjected to a contact reaction; a heavy raw material and a regeneration catalyst are introduced to the upper part reaction zone, such that the heavy raw material and the regeneration catalyst contact the material from the lower part reaction zone. With the method of the present invention, the yield of light oil products (such as gasoline, liquefied gas and diesel) is improved, and the yields of the dry gas and the coke are reduced.

Description

一种烃油转化方法 Hydrocarbon oil conversion process

技术领域 FIELD

[0001] 本发明涉及一种烃油转化的方法,更具体地说,涉及是一种乙烯和丙烯的产率高的烃油转化方法。 [0001] The present invention relates to a process for conversion of a hydrocarbon oil, and more particularly, to a conversion process is a hydrocarbon oil yield of ethylene and propylene.

背景技术 Background technique

[0002] 催化裂化是石油二次加工的重要手段之一,用于从重质原料油生产汽油、柴油、液化气等。 [0002] Catalytic cracking is an important means of secondary oil processing, for heavy feedstock oil to produce gasoline, diesel oil, LPG and the like. 催化裂化工艺采用分子筛催化剂,原料油用水蒸汽雾化并喷入提升管反应器内,与来自再生器的高温催化剂(550-700°C )在提升管中接触反应,一起沿提升管向上,随后离开提升管反应器。 Molecular sieve catalyst cracking process, the feedstock oil atomized with steam and sprayed into the riser reactor, contacting the reaction in the riser and the regenerator catalyst from the high temperature (550-700 ° C), along with the riser upwards, then leaving the riser reactor. 反应产物经在沉降器中分离出催化剂,之后去分馏塔进行产品分离。 The reaction product was separated from the catalyst in the settler, after fractionation column to separate product. 随着催化裂化原料油的重质化,存在的问题是油品的劣质化,轻质油品(如汽油+液化气+柴油)的收率较低,且干气和焦炭的产率较高。 As the catalytic cracking of heavy oil feedstock, there is a problem of poor quality of oil, the lower the yield of light oil (e.g., diesel fuel + LPG + gasoline), and higher yield of dry gas and coke .

发明内容 SUMMARY

[0003] 本发明的目的在于克服现有的烃油转化方法存在的轻质油品(如汽油+液化气+ 柴油)的收率较低且干气和焦炭的产率较高的缺点,提供一种轻质油品(如汽油+液化气+柴油)的收率高且干气和焦炭的产率低的烃油转化方法。 [0003] The object of the present invention to overcome the low yields of light oils (e.g., LPG, gasoline and diesel +) is present in a conventional conversion process of hydrocarbon oils and higher yields of dry gas and coke disadvantages, to provide a lightweight oil (e.g., diesel fuel + LPG + gasoline) in a high yield conversion of a hydrocarbon oil and a low yield of dry gas and coke.

[0004] 本发明提供了一种烃油转化方法,其中,该方法包括: [0004] The present invention we provide a hydrocarbon conversion process oil, wherein the method comprises:

[0005] (1)将预提升介质、柴油原料、以及再生催化剂和/或半再生催化剂送入提升管反应器的下部反应区,在600-750°C的温度下进行接触反应,将生成的油气和反应后的催化剂向上送入提升管反应器的上部反应区; [0005] (1) pre-lifting media, oil feedstock and regenerated catalyst and / or semi-regenerated catalyst to enhance the lower reaction zone into the riser reactor, contacting at a temperature of 600-750 ° C, and the resulting lifting tube into the upper reaction zone of the reactor after the catalyst and hydrocarbon upwardly reaction;

[0006] (2)将重质油原料和再生催化剂送入提升管反应器的上部反应区,在500-650°C 的温度下使所述重质油原料、再生催化剂以及来自下部反应区的油气和催化剂一起进行接触反应; [0006] (2) The heavy oil feedstock and regenerated catalyst into the upper reaction zone lift tube reactor, the heavy oil feedstock at a temperature of 500-650 ° C, and the regenerated catalyst from the lower reaction zone contact reaction with hydrocarbons and catalyst;

[0007] (3)将在上部反应区反应后的油气和催化剂的混合物进行油剂分离,油剂分离后的油气送去后续分离系统分离反应产品,油气分离后的催化剂经汽提后得到待生催化剂; [0007] (3) will be separated in the mixture of hydrocarbon oil and an upper portion of the catalyst after the reaction zone, after separation of the oil and gas sent to the subsequent separation system to separate the reaction product, the catalyst was stripped and the oil separator to be obtained Health catalyst;

[0008] (4)将所述待生催化剂进行烧焦再生,得到再生催化剂,或者在含第一再生器和第二再生器的再生装置中进行烧焦再生,从第一再生器和第二再生器分别得到半再生催化剂和再生催化剂; [0008] (4) burning the spent catalyst regeneration, regenerated catalyst or regenerated in a regenerator for burning the regenerator means comprising first and second regenerator, the regenerator from the first and second The regenerator respectively and semi-regenerated catalyst regenerated catalyst;

[0009] (5)将得到的再生催化剂和/或半再生催化剂返回提升管反应器的下部反应区循环使用,和/或将得到的再生催化剂返回提升管反应器的上部反应区循环使用。 [0009] (5) The resulting regenerated catalyst and / or semi-regenerated catalyst return riser lower reaction zone of the reactor is recycled, and / or the resulting regenerated catalyst return riser upper reaction zone of the reactor is recycled.

[0010] 本发明提供的烃油转化方法通过在具有上部反应区和下部反应区的提升管反应器内,将柴油原料和重质油原料分别与高温催化剂接触反应,从而提高了轻质油品(如汽油+液化气+柴油)的收率,并降低了干气和焦炭的产率。 [0010] hydrocarbon oil conversion process provided by the present invention in a riser reactor having an upper reaction zone and a lower reaction zone, the feedstock and heavy diesel oil feedstock are contacted with the catalyst temperature, thereby improving the light oil (e.g., LPG, gasoline and diesel +) yield, and reducing the yield of dry gas and coke.

附图说明 BRIEF DESCRIPTION

[0011] 图1为本发明实施例1-2中使用的提升管反应器的结构示意图。 [0011] FIG. 1 is a schematic structural riser reactor used in Examples 1-2 of the present embodiment of the invention. 具体实施方式 detailed description

[0012] 本发明提供了一种烃油转化方法,其中,该方法包括: [0012] The present invention we provide a hydrocarbon conversion process oil, wherein the method comprises:

[0013] (1)将预提升介质、柴油原料和再生和/或半再生催化剂送入提升管反应器的下部反应区,在600-750°C的温度下进行接触反应,将生成的油气和反应后的催化剂向上送入提升管反应器的上部反应区; [0013] (1) The pre-stage medium, and reproducing a diesel feedstock and / or semi-regenerated catalyst into the lower reaction zone of the riser reactor, contacting at a temperature of 600-750 ° C, and the generated oil into the upper reaction zone to enhance the reactor after the reaction the catalyst upwardly;

[0014] (2)将重质油原料、再生催化剂送入提升管反应器的上部反应区,在500-650°C的温度下使所述重质油原料、再生催化剂以及来自下部反应区的油气和催化剂一起进行接触反应; [0014] (2) the heavy oil feedstock, the regenerated catalyst into the upper reaction zone lift tube reactor, the heavy oil feedstock at a temperature of 500-650 ° C, and the regenerated catalyst from the lower reaction zone contact reaction with hydrocarbons and catalyst;

[0015] (3)将在上部反应区反应后的油气和催化剂的混合物进行油剂分离,油剂分离后的油气送去后续分离系统分离反应产品,油气分离后的催化剂经汽提后得到待生催化剂; [0015] (3) will be separated in the mixture of hydrocarbon oil and an upper portion of the catalyst after the reaction zone, after separation of the oil and gas sent to the subsequent separation system to separate the reaction product, the catalyst was stripped and the oil separator to be obtained Health catalyst;

[0016] (4)将所述待生催化剂进行烧焦再生,得到再生催化剂,或者在含第一再生器和第二再生器的再生装置中进行烧焦再生,从第一再生器和第二再生器分别得到半再生催化剂和再生催化剂; [0016] (4) burning the spent catalyst regeneration, regenerated catalyst or regenerated in a regenerator for burning the regenerator means comprising first and second regenerator, the regenerator from the first and second The regenerator respectively and semi-regenerated catalyst regenerated catalyst;

[0017] (5)将得到的再生催化剂和/或半再生催化剂返回提升管反应器的下部反应区循环使用,和/或将得到的再生催化剂返回提升管反应器的上部反应区循环使用。 [0017] (5) The resulting regenerated catalyst and / or semi-regenerated catalyst return riser lower reaction zone of the reactor is recycled, and / or the resulting regenerated catalyst return riser upper reaction zone of the reactor is recycled.

[0018] 本发明中,术语“重质油原料”的定义和种类为本领域技术人员所公知,可以为直馏蜡油、减压瓦斯油、加氢裂化尾油、加氢精制油、溶剂脱浙青油、焦化蜡油、常压渣油、减压渣油中的一种或多种。 [0018] the present invention, the term "heavy oil feedstock" is defined and known to those skilled in the type well known, may be a straight run gas oil, vacuum gas oils, hydrocracking tail oil, hydrogenated refined oil, solvents de Zhejiang green oil, coker gas oil, atmospheric residues, vacuum residues of one or more.

[0019] 此外,术语“柴油原料”的定义和种类为本领域技术人员所公知,可以为馏程为180-380°C的石油烃馏分或馏程在180-380°C范围内的石油烃馏分,其中优选馏程为180-330°C的石油烃馏分。 [0019] In addition, the term "diesel feedstock" is defined and known to those skilled in the type well known, may be a distillation range of 180-380 ° C petroleum hydrocarbon fraction or a petroleum hydrocarbon distillation range in the range of 180-380 ° C fractions, preferably a distillation range of 180-330 ° C petroleum hydrocarbon fraction. 以上所述的石油烃馏分可以是原油经一次加工生产的直馏柴油(馏份馏程为180-350°C )、经二次加工生产的柴油馏份(馏份馏程为180-350°C )中的一种或多种的混合物,所述一次加工为原油常压蒸馏,所述二次加工包括催化裂化、焦化、力口氢裂化、加氢处理、加氢精制等。 The above-described petroleum hydrocarbon oil fraction can be produced by machining a straight-run diesel (fraction distillation range 180-350 ° C), produced by the secondary processing of the diesel fraction (fraction distillation range 180-350 ° a medium of C) or more thereof, once processed into the atmospheric distillation of crude oil, comprises the secondary processing catalytic cracking, coking, hydrocracking opening force, hydrotreating, hydrofinishing and the like. 例如,可以为直馏柴油、催化柴油、热裂化柴油、加氢处理柴油、加氢精制柴油、加氢裂化柴油中的一种或多种。 For example, a straight run diesel, catalyzed diesel, thermal cracking diesel, hydrotreated diesel, one or more, diesel hydrotreating, hydrocracking diesel.

[0020] 在本发明中,在更优选的情况下,所述柴油原料与再生催化剂和/或半再生催化剂接触反应的温度可以为620-670°C。 [0020] In the present invention, in the more preferred case, the diesel feed with regenerated catalyst and / or semi-regenerated catalyst to the reaction temperature may be 620-670 ° C. 本发明中,通过将下部反应区的反应温度控制在上述范围内,使柴油原料与再生催化剂和/或半再生催化剂接触,柴油原料进行裂解,从而增加了汽油和液化气的收率;在上部反应区内,重质油原料与再生催化剂以及下部反应区来的物料接触,对重质油原料进行裂解,优化了重质油反应环境,降低了干气和焦炭的收率,增加了总液体收率(汽油+柴油+液化气)的收率。 In the present invention, the reaction temperature of the lower reaction zone by controlled within the above range, diesel feed with regenerated catalyst and / or semi-regenerated catalyst, a diesel feedstock cleavage, thereby increasing the yield of gasoline and LPG; in the upper portion the reaction zone, the heavy oil feed with regenerated catalyst to the reaction zone and the lower material contacting of the heavy oil feedstock for cracking heavy oil to optimize the environment of the reaction, reducing the yield of dry gas and coke increases the total liquid yield yield (LPG + gasoline + diesel) of.

[0021] 根据本发明,所述柴油原料与再生催化剂和/或半再生催化剂接触的压力可以为100-450千帕,优选为观0-320千帕;接触的时间可以为0. 1_10秒,优选为4_8秒。 [0021] According to the present invention, a diesel fuel feedstock and regenerated catalyst and / or semi-regenerated catalyst may be in contact with pressure 100 to 450 kPa, preferably 0-320 kPa concept; contact time may be 0.5 seconds 1_10, preferably 4_8 seconds. 所述柴油原料与再生催化剂和/或半再生催化剂的用量可以在很大范围内改变,优选情况下,所述再生催化剂和/或半再生催化剂与柴油原料的重量比可以为2-30 : 1,更优选为5-10 : 1。 The diesel feed with regenerated catalyst and / or the amount of semi-regenerated catalyst may be varied over a wide range, Preferably, the regenerated catalyst and / or semi-regenerated catalyst and a diesel feedstock weight ratio may be 2-30: 1 , more preferably 5-10: 1.

[0022] 根据本发明,在更优选的情况下,所述重质油原料与再生催化剂接触反应的温度为570-620°C。 [0022] According to the present invention, in the more preferred case, the heavy oil feed with regenerated catalyst to the reaction temperature of 570-620 ° C. 所述重质油原料与再生催化剂接触的压力可以为130-450千帕,优选为150-200千帕;接触的时间可以为0.1-10秒,优选为3-7秒。 The heavy oil feed with regenerated catalyst may be a pressure 130-450 kPa, preferably 150-200 kPa; contact time may be 0.1 to 10 seconds, preferably 3-7 seconds. 所述再生催化剂(新加入的再生催化剂)的用量可以在很大范围内改变,优选情况下,所述再生催化剂与重质油原料的重量比可以为2-15 : 1,更优选为5-10 : 1。 The amount of the regenerated catalyst (regenerated catalyst is newly added) can be varied over a wide range, Preferably, the weight of the regenerated catalyst with the heavy oil feedstock ratio may be 2-15: 1, and more preferably a 5- 10: 1.

[0023] 在本发明中,在所述提升管反应器内,下部反应区与上部反应区的体积之比没有特别的限制,提升管反应器各反应区的直径可以相同,也可以不同,当提升管反应器各反应区的直径相同时,则上部反应区与上部反应区的高度比即为体积比,因此,通过调整升介质的流速,可以控制提升管反应器中反应原料与催化剂的接触时间,优选情况下,所述下部反应区与上部反应区的体积之比1 : 0.2-10,更优选为1 : 6-10。 [0023] In the present invention, said riser reactor, the volume ratio of the lower reaction zone and an upper portion of the reaction zone is not particularly limited, the diameter of each lift tube reactor reaction zone may be the same or different, when diameter of each lift tube reactor reaction zone are the same, the height of the upper portion of the upper reaction zone is the reaction zone volume ratio, thus, by adjusting the flow rate of the medium rise, the contact can be controlled in the reactor riser reactor feed with the catalyst time, preferably, the ratio of the volume of the lower reaction zone and an upper portion of the reaction zone 1: 0.2-10, and more preferably 1: 6-10.

[0024] 根据本发明,所述预提升介质可以是本领域技术人员熟知的各种预提升介质,如水蒸汽、炼油厂干气、轻质烷烃、轻质烯烃中的一种或多种。 [0024] According to the invention, the pre-stage medium may be various well known to those skilled in the pre-lift medium, such as steam, dry refinery gas, light hydrocarbons, light olefins, one or more. 预提升介质的作用是使催化剂加速上升,在提升管反应器底部形成密度均勻的催化剂活塞流。 Pre-action lifting medium is accelerated catalyst, in the riser reactor to form a uniform density of the catalyst at a bottom of the piston. 预提升介质的用量是本领域的技术人员所公知的,优选地,预提升介质的用量占烃油总量的1-30重量%,优选2-15 The amount of pre-lift medium according to the present art is well known in the art, preferably, the pre-lift amount of the medium is 1-30 wt% with an amount of a hydrocarbon oil, preferably 2-15

重量%。 weight%.

[0025] 根据本发明,所述重质油原料与柴油原料之间的比例可以在很大范围内改变,优选情况下,所述重质油原料与柴油原料的重量比可以为0. 1-10 : 1,更优选为0.2-5 : 1, 最优选为2-5 : 1。 [0025] According to the present invention, the ratio between the mass of the heavy oil feedstock oil feedstock may vary within a wide range, Preferably, the heavy oil feedstock with a diesel feedstock weight ratio may be 0. 1- 10: 1, more preferably from 0.2 to 5: 1, and most preferably 2-5: 1.

[0026] 本发明中,所述催化剂为含有分子筛的裂化催化剂,所述裂化催化剂的组成为本领域技术人员所公知,例如,所述裂化催化剂可以含有一种或多种分子筛、耐热无机氧化物,以及选择性含有的粘土;其中,分子筛、耐热无机氧化物和粘土的含量为本领域技术人员所公知。 [0026] In the present invention, the catalyst composition is a molecular sieve containing cracking catalyst, the cracking catalyst known to those skilled in the art, e.g., the cracking catalyst may contain one or more molecular sieves, heat-resistant inorganic oxide was selective and clay contained; wherein the molecular sieves, and heat-resistant inorganic oxide content of the clay are known to those skilled in the art.

[0027] 所述分子筛的种类为本领域技术人员所公知,例如,可以是用作裂解催化剂活性组分的中孔和/或大孔分子筛。 [0027] The type of the molecular sieve known to those skilled in the art, for example, may be used as a mesoporous and / or macroporous molecular sieve cracking catalyst active component. 所述大孔分子筛如含或不含磷元素的Y型沸石、含或不含稀土元素的超稳Y型沸石;所述中孔分子筛为含或不含磷元素的具有五元环结构的高硅沸石、β沸石、丝光沸石、Ω沸石中的一种或多种,具有五元环结构的高硅沸石可以是ZSM-5 沸石和/或ZRP沸石,优选含或不含磷元素的具有五元环结构的ZSM-5沸石和/或ZRP沸石。 The large pore molecular sieve, such as Y-type zeolite-containing or non-phosphorus element-containing ultrastable Y-type zeolite with or without rare earth element; said mesoporous molecular sieve having a five-membered ring structure with or without a high phosphorous element silicalite, zeolite beta], mordenite, one or more Ω zeolite, pentasil zeolites having a ring structure may be a ZSM-5 zeolite and / or ZRP zeolites, preferably containing phosphorous, or a five-element ZSM-5 zeolites and / or ZRP zeolites membered ring structure.

[0028] 所述耐热无机氧化物为本领域技术人员所公知,如可以选自氧化铝、氧化硅、无定型硅铝、氧化锆、氧化钛、氧化硼、碱土金属氧化物中的一种或多种。 [0028] The heat-resistant inorganic oxide well known to those skilled in art, as may be selected from alumina, silica, amorphous silica-alumina, zirconium oxide, titanium oxide, boron oxide, alkaline earth metal oxide of one or more.

[0029] 所述粘土为本领域技术人员所公知,如可以选自高岭土、多水高岭土、蒙脱土、硅藻土、埃洛石、皂石、累脱土、海泡石、凹凸棒石、水滑石、硼润土中的一种或多种。 [0029] The clay known to those skilled in the art, as can be selected from kaolin, halloysite, montmorillonite, diatomaceous earth, halloysite, saponite, tired bentonite, sepiolite, attapulgite water talc, bentonite in one or more.

[0030] 以下参照图1,详细描述本发明的反应过程。 [0030] Referring now to Figure 1, the reaction process of the present invention is described in detail.

[0031] 预热后的柴油原料通过提升管反应器的第一雾化喷嘴5进入下部反应区1的底部,同时再生催化剂和/或半再生催化剂经提升管反应器的第一催化剂入口3进入下部反应区1的底部,在经管线7进入提升管反应器底部的预提升介质的提升作用下,所述再生催化剂和/或半再生催化剂及柴油原料流沿提升管反应器上升并在下部反应区1中接触反应,之后,下部反应区1的反应物流进入上部反应区2。 [0031] The preheated oil feedstock by first lifting atomizing nozzles 5 into the riser reactor 1 at the bottom of the lower reaction zone, while the regenerated catalyst and / or the first catalyst inlet through the semi-regenerated catalyst riser 3 into the reactor the bottom of the lower reaction zone 1 under the action of lifting the bottom via line 7 into the reactor riser is pre-stage medium, the regenerated catalyst and / or semi-regenerated catalyst and a diesel feed flow in a riser reactor to rise and lower reaction contacting the reaction zone 1, then, a lower portion of the reaction zone into the upper stream reaction zone 2.

[0032] 预热后的重质油原料通过提升管反应器的第二雾化喷嘴6进入上部反应区2,同时再生催化剂经提升管反应器的第二催化剂入口4进入上部反应区2,重质油原料与再生催化剂、来自下部反应区1的反应物流在上部反应区2中混合接触反应;之后,上部反应区2的反应物流继续上升至提升管反应器出口后进入沉降分离器,分离催化剂和反应产物,催化剂经汽提器汽提得到待生催化剂,待生催化剂进入再生器烧焦得到再生催化剂,或者进入包括第一再生器和第二再生器的再生装置中进行烧焦再生,从第一再生器和第二再生器分别得到半再生催化剂和再生催化剂。 [0032] After preheating the heavy oil feedstock by lifting a second atomizing nozzle into the reactor 6 the upper reaction zone 2, while the second regenerated catalyst inlet via the riser reactor 4 enters the upper catalyst zone 2, a weight oil feed with regenerated catalyst, the reaction stream from the lower portion of the reaction zone 1 in the upper reaction zone mixing and contacting the reaction 2; then, the upper portion of the reaction zone of the reaction stream 2 continues to rise to lift the reactor outlet into the sedimentation separator, separating the catalyst and the reaction product, the catalyst is stripped spent catalyst is stripped, spent catalyst enters regenerator to obtain regenerated catalyst burning or reproducing apparatus enters the regenerator comprises a first and second regenerator for burning regeneration, from a first regenerator and a regenerator respectively second semi-regenerated catalyst and regenerated catalyst. 再生催化剂和/或半再生催化剂循环使用,反应产物进入后续产品分离设备。 Regenerated catalyst and / or the subsequent product separation device half recycled regenerated catalyst, into the reaction products.

[0033] 在本发明的上述方法中,在汽提器中采用水蒸汽进行汽提,其作用是将催化剂颗粒之间和颗粒孔隙内充满的油气置换出来,提高油品产率。 [0033] In the method of the present invention, the use of steam stripping in the stripper, it is the role of catalyst particles and between the particles within the pores filled with oil and gas displaced, improving oil yield. 用于汽提的水蒸汽的量是本领域的技术人员所公知的。 The amount of water vapor for stripping of skill in the art are well known. 一般来说,用于汽提的水蒸汽的用量占催化剂循环量的0. 1-0.8 重量%,优选0. 2-0. 4重量%。 Generally, 0.5 to 0.8 wt% of the catalyst circulation for stripping steam used in an amount of preferably 0. 2-0. 4 wt%. 术语“循环量” 一般是指单位时间内催化剂在反应-再生系统间传递的重量,此处特指单位时间内通过汽提器的催化剂重量。 The term "circulation amount" refers generally to a unit time of the catalyst in the reaction - weight is transferred between the reproduction system, by weight of the catalyst in the stripper unit time here especially. 由于催化剂在经过一段时间循环后,会有损失,因此,需要定期或不定期地补充新鲜催化剂,将新鲜催化剂通过小型加料系统或其它方式引入再生器中,与再生催化剂混合一起使用。 Since the catalyst after a period of time cycle, there will be losses, thus, the need for regular or irregular intervals to add fresh catalyst, fresh catalyst feed system, or by small otherwise introduced into the regenerator, a regenerated catalyst with mixing.

[0034] 下面结合附图以实施例的方式对本发明作更进一步的详细描述,但不应认为是对本发明所保护的范围的限制。 [0034] DRAWINGS In the embodiments described in detail further embodiment of the present invention, but should not be considered as limiting the scope of the claimed invention.

[0035] 以下实施例中,用于汽提的水蒸汽的用量占催化剂循环量的约0.4重量%,预提升介质采用水蒸汽。 Catalyst circulation is used in an amount from about 0.4 wt. [0035] In the following examples, for stripping% water vapor, by steam pre-stage medium.

[0036] 实施例1 [0036] Example 1

[0037] 本实施例采用中型提升管反应器,该提升管反应器为总高度为10米,直径为25厘米的圆柱体结构,其中,下部、上部反应区的高度比为1 : 7. 5,该提升管最下部即下部反应区的下方为预提升段。 [0037] The present embodiment employs a medium-sized riser reactor, the riser reactor to a total height of 10 meters and a diameter of 25 cm cylindrical structure, wherein the height ratio, a lower portion, an upper portion of the reaction zone is 1: 7.5 , i.e. the lowermost portion of the riser reaction zone is below the lower pre-stage segment.

[0038] 从下部反应区引入柴油原料和再生催化剂,其中,柴油原料为催化柴油,从上部反应区引入重质油原料和再生催化剂,其中,重质油原料为直馏蜡油。 [0038] introduced into the reaction zone from the lower oil feedstock and regenerated catalyst, wherein the feedstock is a diesel catalytic diesel oil, heavy oil feedstock and introducing the regenerated catalyst from the upper portion of the reaction zone, wherein the heavy oil feedstock is a VGO. 直馏蜡油的进料量与催化柴油的进料量的重量比为1 : 2,原料的性质列于表1。 VGO feed with a catalytic quantity of diesel fuel feed amount by weight ratio of 1: 2, the nature of the raw materials shown in Table 1.

[0039] 所使用的催化剂为中国石油化工集团齐鲁催化剂厂生产的牌号为LV-23的催化齐U,其性质列于表2。 [0039] The catalyst used for the China Petrochemical Qilu Catalyst Factory production grades for homogeneous catalysis LV-23 U, its properties are shown in Table 2.

[0040] 具体步骤为,如图1所示,预热后的柴油原料通过第一雾化喷嘴5进入下部反应区1,来自再生器的再生催化剂经第一催化剂入口3进入下部反应区1,柴油原料与再生催化剂(CEP-I)接触,在经管线7进入提升管反应器底部的预提升介质的作用下,沿提升管反应器上升,进入上部反应区2。 [0040] The specific steps are as shown in Figure 1, a diesel preheated feedstock through a first spray nozzle 5 into the lower reaction zone 1, the regenerated catalyst from the regenerator via first catalyst inlet 3 into the lower reaction zone 1, the oil feedstock and regenerated catalyst (CEP-I) in contact, via line 7 into the bottom of the reactor riser to enhance the role of the pre-medium rises along the riser reactor, the reaction zone into the upper 2.

[0041] 预热后的直馏蜡油通过第二雾化喷嘴6进入上部反应区2,来自再生器的再生催化剂经第二催化剂入口4进入上部反应区2,直馏蜡油与再生催化剂(CEP-I)以及来自下部反应区的物流接触反应;来自下部、上部反应区的反应物流沿提升管反应器上升至提升管反应器出口后进入沉降分离器,分离催化剂和反应产物,催化剂经汽提器汽提得到待生催化剂,待生催化剂进入再生器烧焦得到再生催化剂,将再生催化剂循环使用,反应产物进入后续产品分离设备。 [0041] VGO preheated by a second atomizing nozzle 6 into the upper portion of the reaction zone 2, the regenerated catalyst from the regenerator through the catalyst inlet 4 into the upper portion of the second reaction zone 2, the regenerated catalyst with VGO ( CEP-I) and a stream from the lower reaction zone of the contact reaction; the reaction stream from the lower portion, the upper portion of the reaction zone in the riser reactor rises to lift the reactor outlet into the sedimentation separator, catalyst and reaction product separation, catalyst was steam stripper stripped spent catalyst, spent catalyst enters regenerator burning regenerated catalyst, recycled regenerated catalyst, the reaction product into the subsequent product separation equipment.

[0042] 具体的操作条件和产品分布分别列于表3和表4。 [0042] the specific operating conditions and product distribution are listed in Table 3 and Table 4.

[0043] 表1 [0043] TABLE 1

[0044] [0044]

Figure CN102453506AD00071
Figure CN102453506AD00081

[0047] 实施例2 [0047] Example 2

[0048] 根据与实施例1相同的方法进行烃油转化,所不同的是反应条件有所不同。 [0048] The hydrocarbon oil conversion carried out according to the same method as in Example 1, except that the reaction conditions are different. 具体的操作条件和产品分布分别列于表3和表4。 Specific operating conditions and product distribution are listed in Table 3 and Table 4.

[0049] 对比例1 [0049] Comparative Example 1

[0050] 根据与实施例1相同的方法进行烃油转化,所不同的是从反应条件有所不同。 [0050] The hydrocarbon oil conversion carried out according to the same method as in Example 1, except that different from the reaction conditions. 具体的操作条件和产品分布分别列于表3和表4。 Specific operating conditions and product distribution are listed in Table 3 and Table 4.

[0051]表 3 [0051] TABLE 3

[0052] [0052]

Figure CN102453506AD00091

[0053]表 4 [0053] TABLE 4

[0054] [0054]

Figure CN102453506AD00092
Figure CN102453506AD00101

[0055] 从表4结果可以看出,采用本发明提供的方法,可以提高轻质油(如汽油+液化气+柴油)的收率,并降低了干气和焦炭产率。 [0055] As can be seen from the results in Table 4, the method provided by the invention, can increase the yield of light oil (e.g., diesel fuel + LPG + gasoline) and reduces the yield of dry gas and coke.

Claims (11)

  1. 1. 一种烃油转化方法,其特征在于,该方法包括:(1)将预提升介质、柴油原料、以及再生催化剂和/或半再生催化剂送入提升管反应器的下部反应区,在600-750°C的温度下进行接触反应,将生成的油气和反应后的催化剂向上送入提升管反应器的上部反应区;(2)将重质油原料和再生催化剂送入提升管反应器的上部反应区,在500-650°C的温度下,使所述重质油原料、再生催化剂以及来自下部反应区的油气和催化剂一起进行接触反应;(3)将在上部反应区反应后的油气和催化剂的混合物进行油剂分离,油剂分离后的油气送去后续分离系统分离反应产品,油气分离后的催化剂经汽提后得到待生催化剂;(4)将所述待生催化剂进行烧焦再生,得到再生催化剂,或者在含第一再生器和第二再生器的再生装置中进行烧焦再生,从第一再生器和第二再生器分别得到半再生催 A conversion process of hydrocarbon oils, characterized in that the method comprises: (1) pre-lifting media, oil feedstock and regenerated catalyst and / or lower reaction zone into the semi-regenerated catalyst to the riser reactor at 600 carried out at a temperature of -750 ° C the contact reaction, the catalyst was fed to the resulting oil and the reaction upwardly upper reaction zone of the riser reactor; (2) the heavy oil feedstock and regenerated catalyst into the riser reactor oil and gas (3) in the upper portion of the reaction zone after the reaction; upper reaction zone, at a temperature of 500-650 ° C, the heavy oil feedstock, and the regenerated catalyst is contacted with hydrocarbon and catalyst from the reaction of lower reaction zone a mixture of oil and catalyst were separated, sent to the subsequent separation system oil separation of the reaction product, the catalyst was separated oil obtained after stripping of spent catalyst after oil separation; (4) the spent catalyst is burned regeneration, regenerated catalyst or regenerated in a regenerator for burning the regenerator means comprising first and second regenerator, respectively semi-regenerated catalyst from the first regenerator and the second regenerator 剂和再生催化剂;(5)将得到的再生催化剂和/或半再生催化剂返回提升管反应器的下部反应区循环使用,和/或将得到的再生催化剂返回提升管反应器的上部反应区循环使用。 Agent and a regenerated catalyst; (5) regenerated catalyst obtained and / or semi-regenerated catalyst is returned to enhance recycling of lower reaction zone tubular reactor, and / or a regenerated catalyst obtained returning recycle riser upper reaction zone of the reactor .
  2. 2.根据权利要求1所述的方法,其中,所述柴油原料与再生催化剂和/或半再生催化剂接触反应的温度为620-670°C。 The method according to claim 1, wherein said diesel feed with regenerated catalyst and / or semi-regenerated catalyst to the reaction temperature of 620-670 ° C.
  3. 3.根据权利要求1或2所述的方法,其中,所述柴油原料与再生催化剂和/或半再生催化剂接触的压力为100-450千帕,接触的时间为0. 1-10秒。 3. The method of claim 1 or claim 2, wherein said diesel feed with regenerated catalyst and / or semi-regenerated catalyst contacting pressure is 100-450 kPa, a contact time of 0.5 to 10 seconds.
  4. 4.根据权利要求1所述的方法,其中,所述再生催化剂和/或半再生催化剂与柴油原料的重量比为2-30 : 1。 4. The method according to claim 1, wherein the regenerated catalyst and / or the weight of the semi-regenerated catalyst and a diesel feed ratio of 2-30: 1.
  5. 5.根据权利要求1所述的方法,其中,所述重质原料和再生催化剂的接触的压力为130-450千帕、接触的时间为0. 1-10秒。 The method according to claim 1, wherein said heavy feedstock and regenerated catalyst contacts the pressure of 130-450 kPa, a contact time of 0.5 to 10 seconds.
  6. 6.根据权利要求1所述的方法,其中,所述再生催化剂与重质油原料的重量比为2-25 : 1。 6. The method according to claim 1, wherein the weight of the regenerated catalyst with the heavy oil feedstock ratio of 2-25: 1.
  7. 7.根据权利要求1所述的方法,其中,所述重质油原料与柴油原料的重量比为0.1-10 : 1。 The method according to claim 1, wherein the heavy oil feedstock with a diesel feedstock weight ratio of 0.1: 1.
  8. 8.根据权利要求7所述的方法,其中,重质油原料与柴油原料的重量比为0.2-5 : 1。 8. The method according to claim 7, wherein the weight of the heavy oil feedstock and diesel material ratio of 0.2-5: 1.
  9. 9.根据权利要求1所述的方法,其中,所述重质油原料为直馏蜡油、减压瓦斯油、加氢裂化尾油、加氢精制油、溶剂脱浙青油、焦化蜡油、常压渣油和减压渣油中的一种或多种。 9. The method according to claim 1, wherein said feedstock is heavy oil VGO, vacuum gas oils, hydrocracking tail oil, hydrotreated oils, solvent deasphalted Zhejiang green oil, coker gas oil , atmospheric residue and vacuum residue of one or more.
  10. 10.根据权利要求1所述的方法,其中,所述柴油原料为直馏柴油、催化柴油、热裂化柴油、加氢处理柴油、加氢精制柴油、加氢裂化柴油中的一种或多种。 10. The method according to claim 1, wherein the feedstock is diesel straight-run diesel, catalyzed diesel, thermal cracking diesel, hydrotreated diesel, hydrotreated diesel, diesel hydrocracking one or more .
  11. 11.根据权利要求1所述的方法,其中,所述催化剂为含有分子筛的裂化催化剂,所述分子筛为含或不含磷元素的Y型沸石、含或不含稀土元素的超稳Y型沸石、含或不含磷元素的具有五元环结构的高硅沸石、β沸石、丝光沸石、Ω沸石中的一种或多种。 11. The method according to claim 1, wherein the catalyst is a molecular sieve-containing cracking catalyst, the molecular sieve is a Y-type zeolite containing phosphorus element-containing or not, with or without ultra-stable Y-type zeolite is a rare earth element high silica zeolite having five-membered ring structure with or without phosphorus element-containing, zeolite beta], mordenite, zeolite [Omega] or more of one.
CN 201010518936 2010-10-19 2010-10-19 Hydrocarbon oil conversion method CN102453506A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN 201010518936 CN102453506A (en) 2010-10-19 2010-10-19 Hydrocarbon oil conversion method

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN 201010518936 CN102453506A (en) 2010-10-19 2010-10-19 Hydrocarbon oil conversion method

Publications (1)

Publication Number Publication Date
CN102453506A true true CN102453506A (en) 2012-05-16

Family

ID=46037210

Family Applications (1)

Application Number Title Priority Date Filing Date
CN 201010518936 CN102453506A (en) 2010-10-19 2010-10-19 Hydrocarbon oil conversion method

Country Status (1)

Country Link
CN (1) CN102453506A (en)

Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101191068A (en) * 2006-11-21 2008-06-04 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Cracking method for hydrocarbon oil
CN101314736A (en) * 2007-05-31 2008-12-03 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Method for producing high-octane gasoline with bastard crude oil
US20080314799A1 (en) * 2005-12-23 2008-12-25 China Petroleum & Chemical Corporation Catalytic Conversion Method Of Increasing The Yield Of Lower Olefin
CN101362670A (en) * 2007-08-09 2009-02-11 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Catalytic conversion method of propylene preparation
CN101362669A (en) * 2007-08-09 2009-02-11 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Catalytic conversion method of ethylene, propylene and aromatic hydrocarbon preparation
CN101362959A (en) * 2007-08-09 2009-02-11 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Catalytic conversion method for preparing propone and high-octane number gasoline
CN101456782A (en) * 2007-12-13 2009-06-17 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Method for improving propone output during catalytic conversion process
CN101531558A (en) * 2008-03-13 2009-09-16 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Catalytic conversion method for preparing propylene and aromatic hydrocarbons
CN101531923A (en) * 2008-03-13 2009-09-16 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Catalytic conversion method for preparing propylene and high-octane gasoline
EP2142619A1 (en) * 2007-04-30 2010-01-13 Shell Internationale Research Maatschappij B.V. Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock
US20100163455A1 (en) * 2007-04-13 2010-07-01 Hadjigeorge George A Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock

Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20080314799A1 (en) * 2005-12-23 2008-12-25 China Petroleum & Chemical Corporation Catalytic Conversion Method Of Increasing The Yield Of Lower Olefin
CN101191068A (en) * 2006-11-21 2008-06-04 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Cracking method for hydrocarbon oil
US20100163455A1 (en) * 2007-04-13 2010-07-01 Hadjigeorge George A Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock
EP2142619A1 (en) * 2007-04-30 2010-01-13 Shell Internationale Research Maatschappij B.V. Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock
CN101314736A (en) * 2007-05-31 2008-12-03 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Method for producing high-octane gasoline with bastard crude oil
CN101362959A (en) * 2007-08-09 2009-02-11 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Catalytic conversion method for preparing propone and high-octane number gasoline
CN101362670A (en) * 2007-08-09 2009-02-11 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Catalytic conversion method of propylene preparation
CN101362669A (en) * 2007-08-09 2009-02-11 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Catalytic conversion method of ethylene, propylene and aromatic hydrocarbon preparation
CN101456782A (en) * 2007-12-13 2009-06-17 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Method for improving propone output during catalytic conversion process
CN101531558A (en) * 2008-03-13 2009-09-16 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Catalytic conversion method for preparing propylene and aromatic hydrocarbons
CN101531923A (en) * 2008-03-13 2009-09-16 中国石油化工股份有限公司;中国石油化工股份有限公司石油化工科学研究院 Catalytic conversion method for preparing propylene and high-octane gasoline

Similar Documents

Publication Publication Date Title
US20020195373A1 (en) Heavy oil fluid catalytic cracking process
US3894933A (en) Method for producing light fuel oil
US6388161B1 (en) Production of olefins
US7261807B2 (en) Fluid cat cracking with high olefins production
US4624771A (en) Fluid catalytic cracking of vacuum residuum oil
US20060178546A1 (en) Method and apparatus for making a middle distillate product and lower olefins from a hydrocarbon feedstock
EP1046696A2 (en) A catalytic conversion process for producing isobutane and isoparaffin-enriched gasoline
US6495028B1 (en) Catalytic conversion process for producing isobutane and isoparaffin-enriched gasoline
CN1310223A (en) Catalytic converting process for producing low-alkene gasoline and high-yield diesel oil
CN101724430A (en) Method for preparing light-weight fuel oil and propylene from inferior raw oil
CN101850276A (en) Catalyst regeneration method for improving selectivity of catalyst
CN101362669A (en) Catalytic conversion method of ethylene, propylene and aromatic hydrocarbon preparation
US4032432A (en) Conversions of hydrocarbons
CN101928601A (en) Processing method for catalytic cracking heavy oil
US20130001130A1 (en) Dual riser catalytic cracking process for making middle distillate and lower olefins
CN1031834A (en) Hydrocarbon catalytic converting process for manufacturing of lower olefine
CN101463274A (en) Improved hydrocarbon oil hydrotreating and catalytic cracking combined technique
CN101760239A (en) Utilization method of catalytic cracking diesel
CN101362959A (en) Catalytic conversion method for preparing propone and high-octane number gasoline
CN1912065A (en) Catalytic conversion method for preducing more propylene
CN102533322A (en) Method for producing propylene by using Fischer Tropsch synthetic oil in catalytic cracking mode
US20100163455A1 (en) Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock
CN103031148A (en) Catalytic conversion method for processing high-nitrogen raw material
CN101531923A (en) Catalytic conversion method for preparing propylene and high-octane gasoline
CN101062885A (en) Catalytic conversion method for increasing propylene production

Legal Events

Date Code Title Description
C06 Publication
C10 Entry into substantive examination
C12 Rejection of a patent application after its publication