WO2016197537A1 - 一种反冲洗方法及其设计方法和用途 - Google Patents

一种反冲洗方法及其设计方法和用途 Download PDF

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Publication number
WO2016197537A1
WO2016197537A1 PCT/CN2015/094553 CN2015094553W WO2016197537A1 WO 2016197537 A1 WO2016197537 A1 WO 2016197537A1 CN 2015094553 W CN2015094553 W CN 2015094553W WO 2016197537 A1 WO2016197537 A1 WO 2016197537A1
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Prior art keywords
backwashing
oil
slurry bed
slurry
coal
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PCT/CN2015/094553
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English (en)
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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Publication of WO2016197537A1 publication Critical patent/WO2016197537A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
    • 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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • 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
    • 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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/10—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 with moving solid particles
    • C10G49/12—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 with moving solid particles suspended in the oil, e.g. slurries

Definitions

  • the invention relates to a slurry bed backwashing method, a design method thereof and a use thereof, and belongs to the fields of petrochemical industry and coal chemical industry.
  • Heavy oil deep processing technology can not only effectively use 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.
  • adequate and clean utilization of coal resources is an important choice to ensure energy security.
  • refining coal and inferior residual oil are important methods to solve China's energy dilemma.
  • the slurry bed hydrogenation process is the core of direct coal liquefaction and oil-coal mixing.
  • the present invention provides a slurry bed backwashing method.
  • a slurry bed backwashing method characterized in that a self-produced wax oil and/or heavy diesel oil in a slurry bed hydrogenation reaction is transported to a slurry state Equipment and/or piping and/or interfaces that are clogged by coking or intermittent flow in the bed hydrogenation reaction process are used to backflush the coke or plug.
  • Preferred equipment for backwashing includes a slurry bed hydrogenation reactor, a vacuum furnace and/or a separator.
  • the slurry bed hydrogenation reactor comprises a reactor column body, a feed distributor and a circulating blister, the backwashing point comprising a deck of the distribution plate of the feed distributor and the circulating blister.
  • the circulating blister is flushed through a flushing conduit located on the reactor tower, the conduit height being greater than or equal to the circulating blister height.
  • the vacuum furnace is a vertical tubular structure, and the backwashing point is set at the inlet of the vacuum furnace to flush the coking in the pressure reducing furnace tube.
  • the separator comprises a gas phase outlet at the upper part of the cylinder body and a heavy component discharge port at the bottom of the cylinder body, and the portion from the lower end of the cylinder body to the discharge port of the heavy component adopts a cone structure, the taper angle is 40-120°, backwashing The points are the inclined faces on both sides of the gas phase outlet and the tapered structure.
  • Preferred interfaces and conduits for backwashing include conduits for the dead zone due to coking or intermittent use, sampling ports and instrumentation interfaces, and secondary lines for regulating valves, pumps, and the like.
  • a slurry bed backwashing method characterized in that a portion of a self-produced wax oil and/or heavy diesel oil in a slurry bed hydrogenation reaction flows to a device blocked by coking or intermittent flow in a slurry bed hydrogenation reaction process or Used in the pipeline or interface for backwashing plugging, part of which is mixed with some or all of the raw materials to be hydrogenated or a mixture of raw materials and catalyst to obtain a raw material slurry having a reduced viscosity, and the raw material slurry enters the slurry bed hydrogenation reaction Cycle hydrogenation.
  • the wax oil accounts for 4 to 30% by weight of the raw material to be hydrogenated.
  • the kinematic viscosity is not higher than 750 cSt.
  • the use of the above slurry bed backwashing method is characterized by being used for heavy oil hydrogenation process, coal direct liquefaction process and oil coal mixing process, the heavy oil including heavy crude oil, residual oil, catalytic oil slurry, deoiled asphalt and One or more combinations of coal tar, including one or a combination of lignite, bituminous coal, non-sticky coal, which refers to heavy crude oil, residual oil, catalytic slurry
  • One or more combinations of deoiled bitumen and coal tar are combined with one or more of lignite, bituminous coal and non-stick coal as raw materials, and the ratio of oil to coal ranges from 97:3 to 40:60. .
  • the slurry bed backwashing method of the invention utilizes the better fluidity of the wax oil or the heavy diesel oil, and uses some or all of the wax oil or heavy diesel oil produced by the hydrogenation process for the high temperature in the washing hydrogenation process.
  • the high-pressure coking device or the pipe or interface blocked by intermittent use the oil used is a semi-finished product, the industrial cost is low, the material is convenient to take, and the industrial operation is strong. More importantly, since the oil used is one of the products in the slurry bed hydrogenation reaction process, it will not be reversed when the plug is taken out.
  • the rinsing device and the reaction system have a large influence.
  • the rinsed waste is separated directly in the separator. It is especially suitable for heavy crude oil, inferior residual oil hydrogenation or oil coal mixing or direct coal liquefaction process in which the solid heavy material content in the reaction material is large and thus it is easier to coke and block.
  • FIG. 1 is a schematic view showing the backwashing of a wax oil for a slurry bed reactor according to Embodiment 1 of the present invention
  • FIG. 2 is a schematic view showing backwashing of a wax oil for a separator according to Embodiment 2 of the present invention
  • FIG. 3 is a schematic view showing the backwashing of a wax oil for a vacuum furnace according to Embodiment 3 of the present invention
  • FIG. 4 is a schematic view showing the backwashing of a wax oil for a valve according to Embodiment 4 of the present invention.
  • the following examples are slurry bed oil-coal mixing processes in which the fractionated product includes wax oil and the wax oil is passed through a line and a circulation pump to the backwashing point of the following embodiment.
  • FIG. 1 is a schematic illustration of the backwashing of wax oil for a slurry bed reactor of the present embodiment.
  • the self-produced wax oil in this embodiment is used for rinsing a slurry bed reactor blister 3 which is prone to coking in a slurry bed reactor, wherein the blister 3 is used to make unreacted heavy
  • the slag oil or pulverized coal falls into the blister 3 by gravity, flows out of the outside of the tower body along the lower reactor circulation pipe, is pumped by the reactor circulation pump into the circulating feed distributor 2 passing through the tower body, and enters the reaction tower body again. Continue the catalytic hydrogenation and other reactions.
  • An opening is provided on the circumference of the reactor corresponding to the height position of the slurry bed reactor blister 3 as a blister backwashing point 4 to introduce self-produced wax oil, and the inner wall of the rinsing bed reactor blister 3 is coked or left Solid matter.
  • the flushing oil inlet is arranged at the inclined surface of the distribution plate to flush the blockage on the distribution plate surface, so that the feed distributor is unobstructed.
  • the above flushing operation states are all continuous operations.
  • Fig. 2 is a schematic view showing the backwashing of the wax oil for the separator of the present embodiment.
  • the separator gas outlet backwashing point 6 is disposed on both sides of the gas phase outlet and the two separator heavy component outlet backwashing points 7 are uniformly disposed at the bottom heavy component outlet taper structure, and the backwashing medium is in the hydrogenation process in the foregoing process Self-produced wax oil, the state is continuous operation.
  • Fig. 3 is a schematic view showing the backwashing of the wax oil for the reduced pressure furnace of the present embodiment.
  • a decompression furnace flushing point 9 is provided at the inlet of the decompression furnace 8 to introduce backwashing oil.
  • the coking occurs mainly in the decompression furnace tube, and when the coke material in the furnace tube is detected to be flushed, the wax oil is turned on.
  • the rinsing system, the wax oil is the self-produced wax oil in the hydrogenation process in the foregoing process, and the state is intermittent operation.
  • the backwashing wax oil is flushed from the bottom up, and the pressure for flushing the wax oil comes from the circulation pump, and there is no need to separately set the backwash pump.
  • FIG. 4 is a schematic view of the backwashing of the wax oil for the valve of the present embodiment.
  • the valve dead zone flushing point 10 is located closest to the intermittent operation valve, and when the valve is closed, the wax oil backwashing is started, and the wax oil is the self-produced wax in the hydrogenation process in the first embodiment. oil.
  • the rinse oil wax oil in the examples may also be replaced by diesel or a mixture of wax oil and diesel oil. Only diesel is a refined oil, and the washing cost is high.
  • the slurry bed reactor, separator, vacuum furnace, and valve or pipeline may also be other equipment or piping used in heavy oil hydrogenation process, coal direct liquefaction process, and oil coal mixing process.
  • a part of the wax oil may be mixed with the raw material and/or the catalyst to be hydrogenated, and then cyclically hydrogenated, thereby reducing the viscosity of the solid raw material and re-hydrocracking, and fully utilizing the self-produced wax oil.
  • a slurry bed backwashing method of the present invention effectively washes out the blockage where the dead zone is formed by coking or intermittent operation, and does not cause too much damage to the flushing device.
  • the wax oil backwashing method of the invention is applied to equipment or pipelines used in heavy oil hydrogenation process, coal direct liquefaction process and oil coal mixing process.
  • the utility model has the advantages of simple operation, convenient automation control, improved light oil yield, enhanced stability of the operation of the hydrogenation series device, and improved maintenance period, which is of great significance.

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  • Engineering & Computer Science (AREA)
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Abstract

一种反冲洗方法及其设计方法和用途，反冲洗方法包括将自产蜡油的部分或全部流动至因结焦或间断流动而堵塞的设备或管道或接口中用于反冲洗。用于反冲洗的设备包括加氢反应器、减压炉和分离器。所使用的反冲洗方法操作简便，便于自动化控制，提高轻油收率，增强装置运行稳定性，提高加氢系列装置的检修周期。

Description

一种反冲洗方法及其设计方法和用途 技术领域
本发明涉及一种浆态床反冲洗方法及其设计方法和用途，属于石油化工和煤化工领域。
背景技术
近年来，世界石油资源日益短缺，而且石油资源的重质化和劣质化问题越来越明显，但是随着经济的快速增长，社会对石油产品的需求与日俱增。重油深加工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。
同时，我国是一个富煤贫油的国家，为了应对当今石油供需矛盾和贯彻节能减排政策，充分和清洁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，炼制煤和劣质渣油是解决我国能源困境的重要方法。浆态床加氢工艺是煤直接液化和油煤混炼的核心所在。
由于浆态床加氢工艺的操作温度和压力都比较高，结焦和堵塞现象一直以来是困扰本工艺发展的最大难题，如何解决这一问题成为了研究热点，目前提出的各种方法都是如何避免产生结焦和堵塞，但是在这种工艺的长周期运行中结焦和堵塞几乎无法避免，这就需要一种有效的处理结焦和堵塞的反冲洗方法。
发明内容
基于现有技术中存在的问题，本发明提供了一种浆态床反冲洗方法。将自产重质油用于冲洗因结焦或间断流动而产生的堵塞的设备、管道等，疏通效果显著且不会对装置产生太大的操作负荷影响。
本发明的技术方案：
一种浆态床反冲洗方法，其特征在于浆态床加氢反应的自产蜡油和/或重柴油输送至浆态 床加氢反应工艺中的因结焦或间断流动而堵塞的设备和/或管道和/或接口处用于反冲洗结焦物或堵塞物。
优选的用于反冲洗的设备包括浆态床加氢反应器、减压炉和/或分离器。
其中所述浆态床加氢反应器包括反应器塔体、进料分布器和循环泡罩，反冲洗点包括所述进料分布器的分布板的板面以及所述循环泡罩处。所述循环泡罩处通过位于所述反应器塔体上的冲洗管道进行冲洗，所述管道高度高于或等于所述循环泡罩高度。
其中所述减压炉为立式管状结构，反冲洗点设置在减压炉进口处，冲洗减压炉管内的结焦。
其中所述分离器包括位于筒体上部的气相出口和筒体底部的重组分出料口，筒体下端至重组分出料口的部分采用锥形体结构，锥角为40-120°，反冲洗点为所述气相出口两侧和锥形结构的倾斜面。
优选的用于反冲洗的接口和管道包括因结焦或间断使用而产生死区的管道、采样口及仪表接口，调节阀、泵等的副线。
一种浆态床反冲洗方法，其特征在于浆态床加氢反应的自产蜡油和/或重柴油一部分流动至浆态床加氢反应工艺中的因结焦或间断流动而堵塞的设备或管道或接口中用于反冲洗堵塞物，一部分与部分或全部待加氢的原料或原料与催化剂的混合物混合得到黏度降低的原料浆料，所述原料浆料进入所述浆态床加氢反应器循环加氢。
优选的所述蜡油占所述待加氢的原料的质量分数为4-30wt％。
所述原料浆料在温度不高于60℃时，运动黏度不高于750cSt。
以上浆态床反冲洗方法的用途，其特征在于用于重油加氢工艺、煤直接液化工艺和油煤混炼工艺，所述重油包括重质原油、渣油、催化油浆、脱油沥青和煤焦油中的一种或者多种组合，所述煤包括褐煤、烟煤、不粘煤中的一种或者多种组合，所述油煤混炼工艺指以重质原油、渣油、催化油浆、脱油沥青和煤焦油中的一种或者多种组合与褐煤、烟煤、不粘煤中的一种或者多种组合为原料进行加工，油与煤的比例范围为97:3-40:60。
还包括上述浆态床反冲洗方法的设计方法。
本发明的技术效果：
本发明的一种浆态床反冲洗方法，利用蜡油或重柴油的流动性较好的特点，将加氢工艺自产的部分或全部蜡油或重柴油用于冲洗加氢工艺中因高温高压而结焦的装置或因间断使用而堵塞的管道或接口，所用油为半成品、工业成本低，且取材方便，工业操作性强。更重要的是由于所用油为浆态床加氢反应工艺中的产物之一，因此在将堵塞物带出的同时不会对反 冲洗装置和反应体系产生太大影响。冲洗后的废物直接在分离器中分离。特别适合用于反应物料中固体重质物料含量较多因而更容易结焦、堵塞的重质原油、劣质渣油加氢或油煤混炼或煤直接液化工艺中。
附图说明
图1为本发明实施例1的用于浆态床反应器的蜡油反冲洗示意图；
图2为本发明实施例2的用于分离器的蜡油反冲洗示意图；
图3为本发明实施例3的用于减压炉的蜡油反冲洗示意图；
图4为本发明实施例4的用于阀门的蜡油反冲洗示意图。
附图标号：
1-浆态床反应器进料分布板；2-浆态床反应器循环进料分布板；3-泡罩；4-泡罩反冲洗点；5-分离器；6-分离器气体出口反冲洗点；7-分离器重组分出口反冲洗点；8-减压炉；9-减压炉冲洗点；10-阀门死区冲洗点。
具体实施方式
为进一步阐述本发明的具体特征，将结合图1、2、3、4和实施例加以说明。
以下各实施例为浆态床油煤混炼工艺，分馏产物中包括蜡油，并将蜡油通过管路和循环泵与下述实施例的反冲洗点连通。
实施例1
图1为本实施例的用于浆态床反应器的蜡油反冲洗示意图。如图1所示，本实施例中的自产蜡油用于冲洗浆态床反应器中容易产生结焦的浆态床反应器泡罩3，其中所述泡罩3用于使未反应的重质渣油或煤粉通过重力落入泡罩3中，沿下方的反应器循环管流出塔体外部，被反应器循环泵泵入通过塔体内的循环进料分布器2，再次进入反应塔体内，继续进行催化加氢等反应。在反应器圆周上对应于所述浆态床反应器泡罩3的高度位置处设置开口作为泡罩反冲洗点4引入自产蜡油，冲洗浆态床反应器泡罩3内壁上结焦或残留的固体物质。在浆态床反应器进料分布板1和浆态床反应器循环进料分布板2处，由于分布板的板面的网孔较小，容易被固体原料或催化剂堵塞，因此在对应两个分布板斜面处设置冲洗油入口，冲洗分布板面上的堵塞物，使进料分布器通畅。以上冲洗操作状态均为连续操作。
实施例2
图2为本实施例的用于分离器的蜡油反冲洗示意图。如图2所示，在所述分离器5的上 部气相出口的两侧设置分离器气体出口反冲洗点6和在底部重组分出口锥形结构处均匀设置两个分离器重组分出口反冲洗点7，反冲洗介质为前述工艺中加氢工艺中的自产蜡油，状态为连续操作。
实施例3
图3为本实施例的用于减压炉的蜡油反冲洗示意图。如图3所示，在减压炉8的进口处设置减压炉冲洗点9引入反冲洗油，结焦主要发生在减压炉管内，当检测到炉管内的结焦物需要冲洗时启动蜡油反冲洗系统，所述蜡油为前述工艺中加氢工艺中的自产蜡油，状态为间断操作。反冲洗系的蜡油是从下向上冲洗，冲洗蜡油的压力来自于循环泵，无需单独设置反冲洗泵。
实施例4
图4为本实施例的用于阀门的蜡油反冲洗示意图。如图4所示，将阀门死区冲洗点10设在距离间断操作阀门最近处，当阀门关闭时，启动蜡油反冲洗，所述蜡油为实施例1中加氢工艺中的自产蜡油。
实施例中的冲洗油蜡油也可以替换为柴油或蜡油与柴油的混合物。只不过柴油为成品油，冲洗成本高。
所述浆态床反应器、分离器、减压炉以及阀门或管路还可以为重油加氢工艺、煤直接液化工艺和油煤混炼工艺中使用的其它设备或管路。
此外，还可以将一部分蜡油与待加氢的原料和/或催化剂混合后循环加氢，起到了降低固体原料黏度和再次加氢裂化的双重目的，对自产蜡油进行更充分的再利用。
结论：
从上述实施例可以看出，本发明的一种浆态床反冲洗方法，很有效地将因结焦或间断操作而形成死区之处的堵塞物冲洗掉，并且不会对冲洗装置产生太大的操作负荷影响。本发明的蜡油反冲洗方法应用于重油加氢工艺、煤直接液化工艺和油煤混炼工艺中使用的设备或管路。操作简便，且便于自动化控制，提高了轻油收率，增强了加氢系列装置运行的稳定性，提高了检修周期、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，可轻易想到的变化或替换，例如上述实施例的任意组合，以及应用在其它产生结焦的位置，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. 一种浆态床反冲洗方法，其特征在于浆态床加氢反应的自产蜡油和/或重柴油输送至浆态床加氢反应工艺中的堵塞的设备和/或管道和/或接口处用于反冲洗结焦物或堵塞物。
  2. 根据权利要求1所述的一种浆态床反冲洗方法，其特征在于用于反冲洗的设备包括浆态床加氢反应器、减压炉和/或分离器。
  3. 根据权利要求2所述的一种浆态床反冲洗方法，其特征在于所述浆态床加氢反应器包括反应器塔体、进料分布器和循环泡罩，反冲洗点包括所述进料分布器的分布板的板面以及所述循环泡罩处。
  4. 根据权利要求3所述的的一种浆态床反冲洗方法，其特征在于所述循环泡罩处通过位于所述反应器塔体上的冲洗管道进行冲洗，所述管道高度高于或等于所述循环泡罩高度。
  5. 根据权利要求2所述的一种浆态床反冲洗方法，其特征在于所述减压炉为立式管状结构，反冲洗点设置在减压炉进口处，冲洗减压炉管内的结焦。
  6. 根据权利要求2所述的一种浆态床反冲洗方法，其特征在于所述分离器包括位于筒体上部的气相出口和筒体底部的重组分出料口，筒体下端至重组分出料口的部分采用锥形体结构，锥角为40-120°，反冲洗点为所述气相出口两侧和锥形结构的倾斜面。
  7. 根据权利要求1所述的一种浆态床反冲洗方法，其特征在于用于反冲洗的接口包括因结焦或间断使用而产生死区的采样口、仪表接口、调节阀、泵的副线。
  8. 一种浆态床反冲洗方法，其特征在于浆态床加氢反应的自产蜡油和/或重柴油一部分流动至浆态床加氢反应工艺中的结焦或堵塞的设备和/或管道和/或接口中用于反冲洗堵塞物，一部分与部分或全部待加氢的原料或原料与催化剂的混合物混合得到黏度降低的原料浆料，所述原料浆料进入所述浆态床加氢反应器循环加氢。
  9. 根据权利要求1-8任一所述的一种浆态床反冲洗方法的用途，其特征在于用于重油加氢工艺、煤直接液化工艺和油煤混炼工艺，所述重油包括重质原油、渣油、催化油浆、脱油沥青和煤焦油中的一种或者多种组合，所述煤包括褐煤、烟煤、不粘煤中的一种或者多种组合，所述油煤混炼工艺中油与煤的比例范围为97:3-40:60。
  10. 一种浆态床反冲洗设计方法，其特征在于设计浆态床加氢反应的自产蜡油和/或重柴油输送至浆态床加氢反应工艺中的堵塞的设备和/或管道和/或接口处用于反冲洗结焦物或堵塞物。
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