WO2016176976A1 - 一种多重优化的加氢系列方法及其设计方法和用途 - Google Patents

一种多重优化的加氢系列方法及其设计方法和用途 Download PDF

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WO2016176976A1
WO2016176976A1 PCT/CN2015/094219 CN2015094219W WO2016176976A1 WO 2016176976 A1 WO2016176976 A1 WO 2016176976A1 CN 2015094219 W CN2015094219 W CN 2015094219W WO 2016176976 A1 WO2016176976 A1 WO 2016176976A1
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hydrogen
heating furnace
reactor
hydrogenation
temperature
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French (fr)
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李苏安
邓清宇
王坤朋
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北京中科诚毅科技发展有限公司
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/14—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing with moving solid particles
    • C10G45/16—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing with moving solid particles suspended in the oil, e.g. slurries
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/24—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions with moving solid particles
    • C10G47/26—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions with moving solid particles suspended in the oil, e.g. slurries

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  • the invention relates to a multi-optimized slurry bed hydrogenation series method and the use thereof, and belongs to the fields of petrochemical industry and coal chemical industry.
  • Heavy oil hydrogenation technology can not only effectively utilize petroleum resources, but also improve the economic benefits of petroleum processing enterprises.
  • heavy oil processing mainly includes processes such as delayed coking, heavy oil catalytic cracking and residue hydrogenation.
  • the quality of the liquid product of the delayed coker is poor and the coke yield is high.
  • Heavy oil catalytic cracking has high requirements on raw materials and cannot handle inferior residual oil.
  • Residue hydrogenation can treat high-sulfur, high-carbon, high-metal inferior residual oil, while improving liquid yield and quality of liquid products.
  • Residue fixed bed hydrogenation requires high content of heavy metals in the residue, and slurry slurry bed hydrogenation can effectively remove sulfur, nitrogen and heavy metals from the residue.
  • China is a country rich in coal and oil.
  • making full use of coal resources is an important choice to ensure energy security.
  • the use of coal liquefaction technology and oil-coal mixing technology, refining coal and inferior residual oil into light oil is an important method to solve China's energy dilemma.
  • These process technologies belong to the high temperature and high pressure hydrogenation process. In order to ensure the long-term stable operation of the device, a hydrogenation method with excellent performance is needed to ensure the long period of the reactor is in a stable state and reduce the coking phenomenon of the high temperature separator.
  • the hydrogenation mode generally mixes the hydrogen with the raw materials, enters the raw material heating furnace, and directly passes into the first-stage hydrogenation reactor, and does not additionally introduce hydrogen into the secondary reactor or the tertiary reactor and the high-temperature high-pressure separator.
  • the method is simple in process and low in cost, but the temperature of the first-stage reactor is not easy to adjust, and when the reaction heat is too much, and the temperature of the reactor rises above the warning temperature, a large amount of cold hydrogen or cold oil needs to be replenished, and the temperature is too low. Cold or cold oil can destroy the reaction system in the reactor.
  • the hydrogen partial pressure of the secondary or tertiary reactor is insufficient, the conversion rate is lowered, and the multistage reactor is set to reverse A more thorough purpose that should be carried out cannot be achieved.
  • the operating temperature of the high-temperature high-pressure separator is above 400 ° C, and the polycondensation of the asphaltenes generated in the reactor at such a high temperature causes coking reaction, thereby causing coking.
  • the present invention provides a multi-optimized slurry bed hydrogenation process in which hydrogen is divided into two parts and heated separately and then mixed, and the appropriate mixing ratio is adjusted according to the inlet temperature requirements of the hydrogenation reactor. The hydrogenation reactor inlet temperature is stabilized. The use of this hydrogenation process is also provided.
  • a multiple optimized slurry bed hydrogenation series method characterized in that the method comprises the following steps: the hydrogen is divided into two ways of heating, and after mixing with the raw materials, it is heated into a raw material heating furnace to be heated to 330-420 ° C, and all the way into the hydrogen heating. The furnace is heated to 450-580 ° C, and then the stream of the raw material heating furnace outlet is mixed with all or part of the hydrogen of the hydrogen heating furnace outlet and then enters the hydrogenation reactor.
  • the hydrogen gas may include supplemental hydrogen and recycled hydrogen gas, and the recycled hydrogen gas is obtained by refining the hot high-purity gas, and the supplementary hydrogen gas is preferably mixed with the circulating hydrogen gas to be firstly exchanged with the hot high-component gas at the heat exchanger.
  • the two channels are separately heated, and the temperature of the hydrogen after the heat exchange is 300-420 °C.
  • the hydrogenation reactor is a first-stage reactor, and the hydrogen gas at the outlet of the hydrogen heating furnace is mixed with the stream of the raw material heating furnace outlet and then enters the first-stage hydrogenation reactor, and enters the high-temperature high-pressure separator all the way.
  • the hydrogenation reactor is a multi-stage reactor, and the hydrogen gas at the outlet of the hydrogen heating furnace is mixed with the stream of the raw material heating furnace outlet, and then enters the first-stage hydrogenation reactor, and enters the high-temperature high-pressure separator all the way. Including at least one path, each of which is separately mixed with the stream of the first stage advanced reactor inlet and enters the stage reactor.
  • the ratio of hydrogen from the outlet of the hydrogen heating furnace to the primary reactor and the secondary reactor is preferably from 2:1 to 20:1.
  • the hydrogenation reactor is a three-stage reactor, and the hydrogen gas at the outlet of the hydrogen heating furnace enters the tertiary reactor to be 1/10 to 1/2 of the secondary reactor.
  • the ratio of the hydrogen gas split to the hydrogen heating furnace and the raw material heating furnace is preferably from 1 to 30:1.
  • the hydrogen gas at the outlet of the hydrogen heating furnace enters the high temperature and high pressure separator from the bottom, and the hydrogen inlet is disposed below the liquid level of the separator.
  • a multiple optimized slurry bed hydrocracking device characterized in that the hydrogen pipeline is divided into two inlets respectively connecting the hydrogen heating furnace and the raw material heating furnace, and the raw material heating furnace includes an inlet connecting the raw material conveying pipeline, the hydrogen gas
  • the furnace output conduit includes at least one path that merges with the output conduit of the feedstock furnace to communicate with the inlet of the hydrogenation reactor.
  • a heat exchanger is further included, wherein the heat exchanger passes through a high temperature gas pipeline of a high temperature and high pressure separator and a hydrogen gas pipeline, respectively.
  • one of the hydrogen heating furnace output pipes is connected to the high temperature and high pressure separator.
  • the hydrogen heating furnace output line further includes a plurality of paths which are respectively combined with the inlet pipes of the respective advanced reactors and then connected to the advanced reactor.
  • the use of the multiple optimized slurry bed hydrogenation series method and apparatus described above is characterized by being used in a heavy oil hydrogenation process, a coal direct liquefaction process or a coal-oil mixing process, the heavy oil including crude oil, residual oil, and catalytic oil
  • the heavy oil including crude oil, residual oil, and catalytic oil
  • the coal includes one or more of lignite, bituminous coal, non-stick coal, and the ratio of oil to coal ranges from 97:3 to 40:60.
  • the method firstly divides the hydrogen into two parts, and a small part is mixed with the raw materials and heated to be lower than the inlet temperature of the reactor, and most of the heating in the hydrogen heating furnace is separately heated to be higher than the inlet temperature of the reactor, and then the high-temperature hydrogen is mixed with the raw materials and hydrogen.
  • the mixture is mixed before the inlet of the hydrogenation reactor, and the temperature of the hydrogenation reactor inlet is controlled to be controlled by adjusting the mixing temperature of the high-temperature hydrogen by manual or automatic control.
  • the hydrogenation method solves the problem that the temperature of the reaction system or the reactants are not uniform when the temperature is directly added to the reactor by adjusting the temperature, and is especially suitable for the inferior quality of the solid content, the temperature is not uniform even by the existing temperature control method.
  • the heavy (slag) oil hydrogenation process, the coal direct liquefaction process or the oil-coal mixing process can realize the control of the inlet temperature of the hydrogenation reactor, especially the first-stage reactor, and prevent the temperature in the reactor from rising while not The system inside the reactor caused damage.
  • the method fully utilizes the hot high-scoring gas at the outlet of the high-temperature high-pressure separator.
  • the heat of the high-altitude gas with the temperature of up to 350-470 ° C is exchanged with the supplemental hydrogen and the circulating hydrogen to make the hydrogen source preheat before heating separately, thereby saving energy.
  • the hot high-purity gas is purified to obtain circulating hydrogen, which is used for hydrogen source and recycled.
  • the hydrogenation sites include: primary reactor inlet, secondary reactor inlet, high temperature and high pressure separator inlet; tertiary or higher reactor inlet.
  • the problem that the inlet temperature of the first-stage reactor is unstable and the hydrogen partial pressure in the secondary (or tertiary) reactor and the high-temperature high-pressure separator is insufficient is solved.
  • the ratio of the two portions of hydrogen heated separately is determined based on the inlet temperature of the primary reactor.
  • the hydrogen inlet entering the high temperature and high pressure separator is placed below the liquid level of the separator, and the partial pressure of hydrogen is maintained to be equivalent to the partial pressure of hydrogen in the first reactor.
  • the design method design hydrogen is divided into two parts after heating and then mixing to control the feed temperature, and a hydrogen heating furnace is added to separately heat the hydrogen, which can be heated to a higher temperature than the heating of the raw material requires less energy and time. .
  • a small portion of hydrogen is mixed with the feedstock to increase the uniformity of the feedstock and hydrogen. After the two are completely mixed, the temperature is reached to the reactor, so that the temperature in the reactor does not need to be adjusted to ensure the stability of the temperature in the reactor and the uniformity of the reactant system.
  • the separately heated high-temperature hydrogen can separately supply hydrogen to the secondary or tertiary reactor and the high-temperature high-pressure separator to increase the hydrogen partial pressure, thereby simultaneously solving the problem that the multi-stage reactor is insufficiently reacted due to insufficient hydrogen partial pressure.
  • the separator has a problem of polycondensation reaction and coking due to high temperature and low partial pressure of hydrogen.
  • FIG. 1 is a schematic diagram of a hydrogenation process according to an embodiment of the present invention.
  • 1-hydrogen high-gas heat exchanger 2-hydrogen heating furnace; 3-feeding furnace; 4-stage reactor; 5-secondary reactor; 6-high temperature and high pressure separator; 7-supplement of hydrogen; Circulating hydrogen; 9-feedstock; 10-hot high score gas.
  • the reactor in this embodiment is of two stages and is used for oil coal mixing.
  • the specific hydrogenation process is as follows:
  • the hot gas of the high-altitude gas 10 is heat-exchanged at the hydrogen high-gas heat exchanger 1 to 425 ° C hydrogen gas, and the heat after heat exchange is high.
  • the partial gas 10 is purified, it is a circulating hydrogen gas 8.
  • 20% of the hydrogen after the heat exchange is mixed with the coal slurry feed 9 having a mass ratio of 60:40, and then enters the mixture flow of the raw material heating furnace 3 to 365 ° C, and 80% of the hydrogen enters the hydrogen heating furnace 2 to raise the temperature to 535.
  • a portion of the high temperature hydrogen is then mixed with the mixture stream from the feedstock furnace 3 into the inlet of the primary reactor 4, the amount of which is controlled by an automatic control system such that the feed temperature is maintained at 385 ° C; a portion of the high temperature hydrogen is at the secondary
  • the inlet of the reactor 5 is mixed into the primary reactor outlet stream, and the hydrogen feed is 1/15 of the hydrogen feed of the first reactor; a portion of the high temperature hydrogen enters the high temperature and high pressure separator 6 from the bottom, and the partial pressure of hydrogen is 12.0 MPa.
  • the amount of the mixture stream and the high-temperature hydrogen are adjusted by the automatic control system according to the real-time temperature in the reactor, thereby ensuring the stability of the temperature in the first-stage reactor 4 and the uniformity of the reactants, and the secondary reactor. 5 and the hydrogen partial pressure in the high-temperature high-pressure separator 6 also remained stable, and no coking occurred.
  • the multi-optimized slurry bed hydrogenation series method of the present invention is simple and easy to operate, and Easy to automate control.
  • the heating form and the addition position of hydrogen well solve the instability of the inlet temperature of the first-stage reactor, the hydrogen partial pressure of the secondary reactor, and the polycondensation reaction of asphaltene in the high-temperature high-pressure separator.
  • the enhancement of the stability of the operation of the device is enhanced, the maintenance period of the device is improved, and the light oil yield is increased, which is significant.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
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  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

一种多重优化的加氢系列方法及其设计方法和用途，所述加氢方法包括以下步骤：氢气首先在换热器处与高温高压分离器出口气体即热高分气体换热至300-420℃，然后分为两路加热：一路与原料混合后进入原料加热炉加热至330-420℃形成混合物流，一路进入氢气加热炉加热至450-580℃的高温氢气，高温氢气一路与原料加热炉出口的混合物流混合后进入一级加氢反应器，一路与一级加氢反应器出口的物流混合进入二级加氢反应器，一路自底部进入所述高温高压分离器，若反应器为三级或更多，则依次进入。所述方法操作简便且便于自动化控制。氢气的加热形式和加入位置解决了一级反应器入口温度不稳定、二级反应器氢分压不够、分离器内沥青烯发生缩聚反应的问题。

Description

一种多重优化的加氢系列方法及其设计方法和用途 技术领域
本发明涉及一种多重优化的浆态床加氢系列方法及其用途，属于石油化工和煤化工领域。
背景技术
近年来，随着原油开采量的不断增加和常规原油储量的不断减少，原油劣质化趋势越来越严重，原油直接蒸馏得到的中间馏分油及焦化、催化裂化等二次加工得到的中间馏分的S、N含量也相应增加，与此同时，市场对轻质油的不断增加以及人们环保意识的不断增强，环保法律法规对发动机尾气排放要求更加严格，各种燃油标准要求S、N的含量也更加苛刻。如何将硫、氮等杂质含量较高的中间馏分加工成能够满足环保要求的产品是各炼厂所面临的重要问题。
在此现实环境下，重油加氢技术、煤直接液化技术和煤混炼技术越来越受到重视，重油加氢技术不但可以有效利用石油资源，而且能够提高石油加工企业的经济效益。目前重油加工主要有延迟焦化、重油催化裂化和渣油加氢等工艺。延迟焦化装置的液体产物的质量差、焦炭产率高。重油催化裂化对原料的要求较高，无法处理劣质的渣油。渣油加氢可以处理高硫、高残炭、高金属的劣质渣油，同时提高液收率和液体产物的质量。渣油固定床加氢对渣油中的重金属含量要求较高，渣油浆态床加氢可以有效的脱除渣油中的硫、氮和重金属。
我国是一个富煤贫油的国家，在应对当今石油供需矛盾和贯彻节能减排政策中，充分利用煤炭资源是保障能源安全的重要选择。采用煤液化技术和油煤混炼技术，炼制煤和劣质渣油转化为轻质油是解决我国能源困境的重要方法。这些工艺技术都属于高温高压加氢工艺，为保证装置长周期稳定运行，需要一种性能优良的加氢方法，以保证反应器长周期处于稳定状态，并且减少高温分离器的结焦现象。
目前，加氢方式一般将氢气与原料混合后进入原料加热炉加热，并直接通入一级加氢反应器，没有向二级反应器或三级反应器以及高温高压分离器额外通入氢气。此方式工序简单、成本低，但是一级反应器的温度不易调节，在反应放热过多而导致反应器温度升高超过警戒温度时需要补充大量的冷氢或冷油，而温度过低的冷氢或冷油会破坏反应器内的反应体系。另外，随着反应的进行二级或三级反应器的氢分压不足，转化率降低，设置多级反应器使反 应进行的更加彻底的目的就无法达到。而且高温高压分离器的操作温度在400℃以上，由于在反应器中生成的沥青烯在如此高温下会发生缩聚反应，进而造成结焦。
发明内容
基于现有技术中存在的问题，本发明提供了一种多重优化的浆态床加氢方法，将氢气分为两部分分别加热后再混合，根据加氢反应器入口温度要求调节适当混合比例以使加氢反应器入口温度稳定。还提供了该加氢方法的用途。
本发明的技术方案：
一种多重优化的浆态床加氢系列方法，其特征在于所述方法包括以下步骤：氢气分为两路加热，一路与原料混合后进入原料加热炉加热至330-420℃，一路进入氢气加热炉加热至450-580℃，然后所述原料加热炉出口的物流与所述氢气加热炉出口的全部或部分氢气混合后进入加氢反应器。
所述氢气可包括补充氢气和循环氢气，所述循环氢气由热高分气体精制获得，所述补充氢气与循环氢气混合后优选的首先在换热器处与热高分气体换热后再分为两路分别加热，所述换热后的氢气的温度为300-420℃。
优选的所述加氢反应器为一级反应器，所述氢气加热炉出口的氢气一路与所述原料加热炉出口的物流混合后进入一级加氢反应器，一路进入高温高压分离器。
优选的所述加氢反应器为多级反应器，所述氢气加热炉出口的氢气一路与所述原料加热炉出口的物流混合后进入一级加氢反应器，一路进入高温高压分离器，还包括至少一路，每一路分别与其中一级高级反应器入口的物流混合后进入该级反应器。
所述氢气加热炉出口的氢气进入一级反应器和二级反应器的比例优选为2:1-20:1。
进一步优选的所述加氢反应器为三级反应器，所述氢气加热炉出口的氢气进入三级反应器为进入二级反应器的1/10-1/2。
分流至所述氢气加热炉与所述原料加热炉的所述氢气的比例优选为1-30：1。
优选的所述氢气加热炉出口的氢气自底部进入所述高温高压分离器，且氢气进口设在所述分离器的液面以下。
一种多重优化的浆态床加氢裂化装置，其特征在于氢气管道分为两路分别连通氢气加热炉和原料加热炉的入口，所述原料加热炉包括连通原料输送管道的入口，所述氢气加热炉输出管道至少包括一路，其与原料加热炉的输出管道汇合后连通加氢反应器的入口。
优选的还包括换热器，所述换热器中分别通过高温高压分离器的热高分气体管道和与氢气管道。
优选的所述氢气加热炉输出管道的一路连通高温高压分离器。
当所述加氢反应器为多级反应器，所述氢气加热炉输出管道的还包括若干路，其分别与各高级反应器的入口管道汇合后再连通高级反应器。
以上所述多重优化的浆态床加氢系列方法和装置的用途，其特征在于用于重油加氢工艺、煤直接液化工艺或油煤混炼工艺，所述重油包括原油、渣油、催化油浆、脱油沥青、煤焦油的一种或者多种；所述煤包括褐煤、烟煤、不粘煤中的一种或者多种，油与煤的比例范围为97:3-40:60。
还包括上述多重优化的浆态床加氢系列方法以及装置的设计方法。
本发明的技术效果：
本方法首先将氢气分为两部分加热，少部分与原料混合后加热至低于反应器入口温度，大部分在氢气加热炉单独加热至高于反应器入口温度，然后将高温氢气与原料和氢气的混合物在加氢反应器入口前混合，通过人工或自动控制调节高温氢气的加入量调节混合温度从而控制加氢反应器入口的温度稳定。本加氢方法解决了向反应器中直接加入冷氢等调节温度时导致反应体系温度或反应物不均匀的问题，且尤其适用于固体含量较高、采用现有控温方式温度不易均匀的劣质重(渣)油加氢工艺、煤直接液化工艺或油煤混炼工艺，可实现对加氢反应器特别是一级反应器入口温度的控制，防止反应器内温度升高的同时不会对反应器内的体系造成破坏。
本方法充分利用高温高压分离器出口的热高分气体，一方面温度高达350-470℃的热高分气体与补充氢气和循环氢气换热使氢气源在分别加热前预热，节约能源。另一方面热高分气体经提纯净化后制得循环氢气，用于氢气源，循环使用。
若加氢反应器为二级或以上，则自氢气加热炉出口的氢气的加氢位置相应增加。加氢部位包括：一级反应器入口，二级反应器入口，高温高压分离器入口；三级或更高级反应器入口。同时解决了一级反应器入口温度不稳定以及二级(或三级)反应器、高温高压分离器内的氢分压不够的问题。
分别加热的两部分氢气的比例根据一级反应器入口温度确定。
进入高温高压分离器的氢气进口设在分离器的液面以下，维持氢气分压与一级反应器内氢气分压相当。
本设计方法设计氢气分为两部分加热后再混合的方式控制进料温度，增设了一个氢气加热炉单独对氢气加热，相对于对原料加热需要更少的能量和时间就可加热至更高温度。少部分氢气与原料混合增加原料与氢气的均匀程度。二者完全混合后达到合适的温度再进入反应器，使得反应器内的温度无需再进行调整，保证反应器内温度的稳定和反应物体系的均匀。另外，单独加热的高温氢气可分别对二级或三级反应器以及高温高压分离器额外提供氢气，增加氢分压，从而同时解决了多级反应器因氢分压不够而反应不充分的问题以及分离器因温度高、氢分压低而导致沥青烯发生缩聚反应、结焦的问题。
附图说明
图1为本发明实施例的加氢流程简图。
附图标号：
1-氢气高分气换热器；2-氢气加热炉；3-原料加热炉；4-一级反应器；5-二级反应器；6-高温高压分离器；7-补充氢气；8-循环氢气；9-原料；10-热高分气体。
具体实施方式
为进一步阐述本发明的具体内容，将结合图1和具体实施例详细说明。
本实施例中的反应器为两级，用于油煤混炼，具体加氢流程如下：
补充氢气7与循环氢气8混合后与470℃的高温高压分离器6出口气体即热高分气体10在氢气高分气换热器1处换热升温至425℃氢气，换热后的热高分气体10精制后即为循环氢气8。然后换热后的20％的氢气与质量比为60:40的油煤浆进料9混合后进入原料加热炉3升温至365℃的混合物流，80％的氢气进入氢气加热炉2升温至535℃的高温氢气。然后一部分高温氢气与来自所述原料加热炉3的混合物流混合中进入一级反应器4入口，二者的量通过自动控制系统进行控制使得进料温度保持为385℃；一部分高温氢气在二级反应器5入口混入一级反应器出口物流，氢气进料为一级反应器氢气进料的1/15；一部分高温氢气从底部进入高温高压分离器6，氢分压为12.0MPa。
本实施例在反应过程中，混合物流与高温氢气的量根据反应器内的实时温度由自控系统进行调配，保证了一级反应器4内温度的稳定和反应物的均匀，同时二级反应器5和高温高压分离器6内氢分压也保持稳定，且未发生结焦现象。
结论：
从上述实施例可以看出，使用本发明的多重优化的浆态床加氢系列方法，操作简便，且 便于自动化控制。氢气的加热形式和加入位置很好的解决了一级反应器入口温度不稳定、二级反应器的氢分压不够、高温高压分离器内沥青烯缩聚反应的发生。增强了提高了装置运行的稳定性，提高了装置的检修周期，增加了轻油收率，意义重大。
以上所述仅为本发明较佳的具体实施方式，但本发明的保护范围并不局限于此，任何熟悉本技术领域的技术人员在本发明揭露的技术范围内，可轻易想到反应器级数的变化或氢气源的替换，都应涵盖在本发明的保护范围之内。因此，本发明的保护范围应该以权利要求书的保护范围为准。

Claims (10)

  1. 一种多重优化的浆态床加氢系列方法，其特征在于所述方法包括以下步骤：氢气分为两路加热，一路与原料混合后进入原料加热炉加热至330-420℃，一路进入氢气加热炉加热至450-580℃，然后所述原料加热炉出口的物流与所述氢气加热炉出口的全部或部分氢气混合后进入加氢反应器。
  2. 根据权利要求1所述的方法，其特征在于所述氢气包括补充氢气和循环氢气，所述循环氢气由热高分气体精制获得，所述补充氢气与循环氢气混合后首先在换热器处与热高分气体换热后再分为两路分别加热，所述换热后的氢气的温度为300-420℃。
  3. 根据权利要求1所述的方法，其特征在于所述加氢反应器为一级反应器，所述氢气加热炉出口的氢气一路与所述原料加热炉出口的物流混合后进入一级加氢反应器，一路进入高温高压分离器。
  4. 根据权利要求1所述的方法，其特征在于所述加氢反应器为多级反应器，所述氢气加热炉出口的氢气一路与所述原料加热炉出口的物流混合后进入一级加氢反应器，一路进入高温高压分离器，还包括至少一路，每一路分别与其中一级高级反应器入口的物流混合后进入该级反应器。
  5. 一种多重优化的浆态床加氢裂化装置，其特征在于氢气管道分为两路分别连通氢气加热炉和原料加热炉的入口，所述原料加热炉包括连通原料输送管道的入口，所述氢气加热炉输出管道至少包括一路，其与原料加热炉的输出管道汇合后连通加氢反应器的入口。
  6. 根据权利要求6所述的装置，其特征在于还包括换热器，所述换热器中分别通过高温高压分离器的热高分气体管道和氢气管道。
  7. 根据权利要求5或6所述的装置，其特征在于所述氢气加热炉输出管道的一路连通高温高压分离器。
  8. 根据权利要求5或6所述的装置，其特征在于，所述加氢反应器为多级反应器，所述氢气加热炉输出管道的还包括若干路，其分别与各高级反应器的入口管道汇合后再连通高级反应器。
  9. 权利要求1-4所述的一种多重优化的浆态床加氢系列方法的用途，其特征在于用于重油加氢工艺、煤直接液化工艺或油煤混炼工艺，所述重油包括重质原油、渣油、催化油浆、脱油沥青、煤焦油的一种或者多种；所述煤包括褐煤、烟煤、不粘煤中的一种或者多种，所述油煤混炼工艺中油与煤的比例范围为97:3-40:60。
  10. 一种多重优化的浆态床加氢系列设计方法，其特征在于设计氢气分为两路加热：一 路与原料混合后进入原料加热炉加热至330-420℃，一路进入氢气加热炉加热至450-580℃，然后所述原料加热炉出口的物流与所述氢气加热炉出口的全部或部分氢气混合后进入加氢反应器。
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