CN109663547B - 用于限制固体沉积在具有锥形底部的装备中的现象的包括液体的横向注射件的设备 - Google Patents

用于限制固体沉积在具有锥形底部的装备中的现象的包括液体的横向注射件的设备 Download PDF

Info

Publication number
CN109663547B
CN109663547B CN201811189527.8A CN201811189527A CN109663547B CN 109663547 B CN109663547 B CN 109663547B CN 201811189527 A CN201811189527 A CN 201811189527A CN 109663547 B CN109663547 B CN 109663547B
Authority
CN
China
Prior art keywords
liquid
injection
angle
diameter
cylindrical upper
Prior art date
Legal status (The legal status 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 status listed.)
Active
Application number
CN201811189527.8A
Other languages
English (en)
Other versions
CN109663547A (zh
Inventor
B.安布拉尔
J.马克
J-F.勒科
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
IFP Energies Nouvelles IFPEN
Original Assignee
IFP Energies Nouvelles IFPEN
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
Application filed by IFP Energies Nouvelles IFPEN filed Critical IFP Energies Nouvelles IFPEN
Publication of CN109663547A publication Critical patent/CN109663547A/zh
Application granted granted Critical
Publication of CN109663547B publication Critical patent/CN109663547B/zh
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • 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
    • C10G75/00—Inhibiting corrosion or fouling in apparatus for treatment or conversion of hydrocarbon oils, in general
    • 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
    • B01J8/224—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 the particles being subject to a circulatory movement
    • B01J8/228—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 the particles being subject to a circulatory movement externally, i.e. the particles leaving the vessel and subsequently re-entering it
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2455—Stationary reactors without moving elements inside provoking a loop type movement of the reactants
    • B01J19/2465—Stationary reactors without moving elements inside provoking a loop type movement of the reactants externally, i.e. the mixture leaving the vessel and subsequently re-entering it
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
    • 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
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/085—Feeding reactive fluids
    • 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
    • B01J8/1881—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving downwards while fluidised
    • 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
    • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
    • C10G51/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only
    • C10G51/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only including only thermal and catalytic cracking steps
    • 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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/10—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only cracking steps
    • 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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
    • 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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
    • C10G67/0454—Solvent desasphalting
    • C10G67/049—The hydrotreatment being a hydrocracking
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00893—Feeding means for the reactants
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00245—Avoiding undesirable reactions or side-effects
    • B01J2219/00247—Fouling of the reactor or the process equipment
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00245—Avoiding undesirable reactions or side-effects
    • B01J2219/00252—Formation of deposits other than coke
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/18—Details relating to the spatial orientation of the reactor
    • B01J2219/185—Details relating to the spatial orientation of the reactor vertical
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/19—Details relating to the geometry of the reactor
    • B01J2219/194—Details relating to the geometry of the reactor round
    • B01J2219/1941—Details relating to the geometry of the reactor round circular or disk-shaped
    • B01J2219/1943—Details relating to the geometry of the reactor round circular or disk-shaped cylindrical
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/19—Details relating to the geometry of the reactor
    • B01J2219/194—Details relating to the geometry of the reactor round
    • B01J2219/1941—Details relating to the geometry of the reactor round circular or disk-shaped
    • B01J2219/1946—Details relating to the geometry of the reactor round circular or disk-shaped conical
    • 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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/06—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by pressure distillation
    • C10G9/08—Apparatus therefor
    • C10G9/12—Removing incrustation
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
    • C10G9/16—Preventing or removing incrustation
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/28—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material
    • C10G9/32—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material according to the "fluidised-bed" technique

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

本发明涉及一种在装备(1)底部用于包含固体颗粒的含烃液体下降流的设备，装备(1)包括直径为D1的圆柱形上部(11)、具有相对于所述圆柱形上部的垂直轴(z)为5°至85°的倾斜角α的截锥形下部(12)、直径为D2的出口管(9)，特征在于所述设备包括至少一个使再循环的和/或补充的液体进入装备(1)的截锥形部分(12)中的注射件(5)；至少一个使再循环的和/或补充的液体进入装备(1)的圆柱形部分(11)中的注射件(6)；位于所述截锥形部分中的一个或多个所述注射件(5)相对于截锥形下部的壁在垂直面(xz)中以角度β1倾斜并在水平面(xy)中以角度β2倾斜；位于所述圆柱形部分中的一个或多个所述注射件(6)相对于所述圆柱形上部的壁在垂直面(xz)中以角度θ1倾斜并在水平面(xy)中以角度θ2倾斜，角度β1和θ1为5°至175°，角度β2和θ2为90°至270°。本发明还涉及一种实施所述设备的含烃原料的转化方法。

Description

用于限制固体沉积在具有锥形底部的装备中的现象的包括液 体的横向注射件的设备
发明的技术领域
本发明涉及降低在优选具有锥形底部的分离和蒸馏装备中沉降物或不稳定或不可溶分子的沉积，所述分离和蒸馏装备在处理重质或积垢产物的精炼方法的下游使用。本发明非限制性地涉及生产能够使装备积垢的液体的方法，所述积垢例如减粘裂化、沸腾床中的加氢裂化、催化裂化、油产品精炼中的延迟焦化，以及涉及煤液化和生物质处理的方法。
现有技术
降低使装备积垢的沉积为在用于处理或转化含烃原料，特别是重质原料的装置中的主要问题。实际上，装备积垢需要使装置停止并将其拆卸从而进行清洗。在沸腾床中转化含烃原料的装置中，具体地，分离装备的壁和底部积垢可能是由于具有絮凝而形成固体沉积的沥青质性质的颗粒、吸附至壁上的分子、焦炭颗粒、催化剂粉末、基于镍、铁和/或钒的金属硫化物或更普遍地包含在经处理的含烃原料中的任何固体。
专利申请US 4,534,851 A记载了一种将液体含烃原料引入通至反应器的传输管线的方法，包括以具有分离的同轴料流的上升流形式注射蒸汽和含烃原料，所述含烃原料的料流为内部料流和蒸汽料流为外围料流，并且一部分蒸汽的方向朝向所述传输管线的内壁，而其余的蒸汽和含烃原料以平行于纵轴的方向从该区域排出。
然而，这个申请没有记载通过使截锥形部分内和/或装备的圆柱形部分内含烃液体或外部补充液体再循环而能够使污浊区域减少的设备。
发明内容
本发明涉及一种在装备(1)底部用于包含固体颗粒的含烃液体下降流的设备，装备(1)包括直径为D1的圆柱形上部(11)、具有相对于所述圆柱形上部的垂直轴(z)为5° 至85°的倾斜角α的截锥形下部(12)、直径为D2的出口管(9)，特征在于所述设备包括：
- 至少一个使再循环的和/或补充的液体进入装备(1)的截锥形部分(12)中的注射件(5)；
- 至少一个使再循环的和/或补充的液进入装备(1)的圆柱形部分(11)中的注射件(6)；
位于所述截锥形部分中的一个或多个所述注射件(5)相对于截锥形下部的壁在垂直面(xz)中以角度β1倾斜并在水平面(xy)中以角度β2倾斜；位于所述圆柱形部分中的一个或多个所述注射件(6)相对于所述圆柱形上部的壁在垂直面(xz)中以角度θ1倾斜并在水平面(xy)中以角度θ2倾斜，角度β1和θ1为5°至175°，角度β2和θ2为90°至270°。
有利地，根据本发明的设备包括用于再循环离开所述出口管(9)的一部分液体的管(4)，所述再循环管(4)供应再循环液体至所述注射件(5)或(6)的至少一个。
根据本发明的设备可以包括供应补充液体至所述注射件(5)或(6)的至少一个的补充管(10)。
所述注射件可以分别通过截锥形部分中的水平层(7)和通过圆柱形部分中的水平层(8)分配。
有利地，圆柱形部分的直径D1和截锥形部分底部的出口管的直径D2之间的比率(D1/D2)为1.1至1000，优选2至500，优选3至100。
有利地，角度α为10°至70°，优选15°至60°，非常优选30°至50°。
优选地，角度β1和θ1为10°至150°，非常优选15°至120°，更优选15°至90°，并还更优选20°至60°。
优选地，角度β2和θ2为90°至180°。
非常优选地，角度β2和θ2等于90°。
有利地，直径D1为0.1 m至30 m，优选0.5 m至20 m，非常优选1 m至10 m。
有利地，两个水平层之间的高度H为0.01 m至10 m，优选0.05 m至5 m，非常优选0.1 m至1 m。
优选地，每层的注射件的数目N为1至30个。
优选地，每层注射件的数目为2至20个，同一层内的所述注射件以等于360/N的角度δ间隔开，其中N表示每层的注射件数目。
非常优选地，每层的注射件的数目为2至10个，更优选2至6个。
优选地，所述装备(1)为能够处理含烃原料的分离气体/液体的装置。
本发明还涉及实施所述设备的含烃原料的转化方法。
优选地，所述方法在用于含烃级分的原料的沸腾床中实施加氢转化步骤，所述烃级分的至少50重量%具有高于300℃的沸点。
注入所述注射件中的液体的速度V有利地为0.05 m.s-1至40 m.s-1，优选0.1 m.s-1至30 m.s-1，非常优选0.5 m.s-1至10 m.s-1。
通过注射件(5)和(6)注射的的液体相对于在装备(1)中循环的液体的注射率有利地为1%至400%，优选5%至100%，非常优选10%至60%，更优选20至50%。
附图的简要说明
根据本发明的设备的其他特征和优点在参照下文附图阅读下文的非限制性实施方案实施例的描述之后变得明显。
图1：图1示出根据本发明的设备的示意图。
图2：图2示出装备的圆柱形和截锥形部分内的再循环的含烃液体和/或补充的液体的注射件的使用。
图3：图3示出根据本发明的设备和使液体进入装备的圆柱形和截锥形部分中的多个横向注射件的使用—前视图和顶视图：(3A)进入装备1的圆柱形部分的多个注射件(6)；(3B)进入装备1的截锥形部分中的多个注射件(5)。
图4：图4（4A：等距视图4B：顶视图）示出没有注射件的构型，—其中固相的体积分数大于0.1体积%的装备的部分。这些区域示出积累了固体颗粒的区域。
图5：图5示出具有注射件的构型，—其中固相的体积分数大于0.1体积%的装备的部分。
具体实施方式
一般而言，本发明涉及其中含烃液体在固体颗粒能够在装备底部结垢和积累的情况下循环的任何装备。更具体地，根据本发明的设备位于常压或减压蒸馏塔、分离鼓或能够处理含烃原料的气体/液体分离的任何其他装置的下部。
在文本的其余部分中，“注射件”是指能够将液体从装备壁注入内部的本领域的技术人员已知的任何装置，所述装置以至少一个输送液体的管的形式供应。
图1示出本发明的示意图。
本发明在具有锥形底部的装备(1)中实施，即装备(1)包括圆柱形上部(11)和截锥形下部(12)，其中积垢含烃液体(2)（即包含能够絮凝或吸附在壁上的固体颗粒或化合物的液体）以从装备顶部的下降方式流动并通过出口管(9)离开。截锥形构型是本领域技术人员熟知的通过借助重力促使固体排至出口管而最小化底部沉积。
为了降低装备的壁上和底部中沉积的形成，所述设备包括再循环的和/或补充的液体的横向注射件：进入截锥形部分的注射件(5)和进入圆柱形部分的注射件(6)。这些注射件能够沿着截锥形部分中的水平层(7)和沿着圆柱形部分中的水平层(8)分配至壁上。流出的液体料流通过排放管(3)从装备排出。
在本发明的第一实施方案中，液体（其能够为稀释液）的补充管(10)供给位于截锥形部分中和圆柱形部分中的横向注射件(5)和(6)，从而减少装备(1)中的污浊区域并限制在壁上固体颗粒的沉积。沸点高于或等于供应装备(1)的含烃液体的沸点的任何馏分，例如催化裂化流出物(HCO)、LCO、或任何其他VGO、AR、VR、DAO馏分、芳族提取物，能够适合作为补充液体。根据这个实施方案，通过排放管(3)离开的液体的流速等于在装备中循环的含烃液体(2)的流速和注入补充管(10)中的补充液体的流速的总和。通过补充管(10)注入的补充液体能够通过在装备(1)中产生湍流减少污浊区域从而限制壁上的固体颗粒的沉积。当所选液体为基于芳族时，所述注入的补充液体也能够充当稀释液。
根据本发明的另一实施方案，离开装备(1)的一部分含烃液体能够再循环从而供应横向注射件(5)和(6)。根据这个实施方案，通过排放管(3)离开的液体的流速等于液体(2)的流速。通过再循环管(4)再循环的液体能够通过形成湍流而减少装备(1)中的污浊区域从而限制壁上固体颗粒的沉积。
根据本发明的最后的实施方案，注入横向注射件(5)和(6)的液体可以源自再循环管(4)和源自补充液体管(10)二者。根据这个实施方案，通过排放管(3)离开的液体的流速等于在装备中循环的含烃液体（称为积垢液）(2)的流速和注入补充管(10)中的补充液的流速的总和。通过补充管(10)和通过再循环管(4)注入的液体能够通过在装备(1)中产生湍流减少污浊区域从而限制壁上固体颗粒的沉积并还能够充当前文所述的稀释液。
通过横向注射件(5)和(6)注入的液体因此可以为从装备(1)再循环的液体和/或补充液体，即源自装备(1)外部的液体。
通过横向注射件(5)和(6)注入的液体的注射率定义为在再循环管(4)中液体的流速和在补充管(10)中液体的流速的总和与在装备中循环的含烃液体或积垢液(2)的流速的比率。
进入设备的原料可以包含源自加氢转化工艺的流出物，例如源自H-OIL ™沸腾床装置的任何类型的化合物，还包含源自淤浆加氢转化工艺、源自固定床、移动床、流化床加氢处理工艺的任何类型的化合物、催化裂化(FCC)流出物、来自热转化工艺例如焦化、减粘裂化和任何其他分离工艺例如溶剂脱沥青的流出物。
固体颗粒可以为沉积的沥青质、负载或不负载的催化剂粉末（通常具有小于500微米的直径）或焦炭颗粒、金属例如镍、钒、铁、钼的硫化物。
设备中的流体是下降的，根据本发明的设备可以在减压蒸馏塔底部或在常压塔底部或在任何气体-液体分离器底部使用。
图2示出液体的再循环部分或补充液体的不同类型的横向注射件。
装备1，其例如可以为蒸馏塔或分离器，具有直径为D1的圆柱形上部(11)、截锥形下部(12)、直径为D2的位于装备底部的出口管(9)，其中含烃液体通过其离开。截锥形部分(12)（也称为锥形底部）具有相对于圆柱形部分的垂直壁（由z轴表示）为α的倾斜角。（补充或再循环的）液体的两种类型的注射件定义为：
Figure 506069DEST_PATH_IMAGE001
进入装备(1)的截锥形部分中的注射件(5)。
Figure 485527DEST_PATH_IMAGE001
进入装备(1)的圆柱形部分中的注射件(6)。
位于截锥形部分(12)中的注射件(5)相对于锥形底部的壁在垂直面(xz)中以角度β1倾斜和在水平面(xy)中以角度β2倾斜，x表示水平轴，z表示垂直于水平面(xy)的圆柱形部分的垂直轴。
位于圆柱形部分(11)中的注射件(6)相对于圆柱形体壁在垂直面(xz)中以角度θ1倾斜和在水平面(xy)中以角度θ2倾斜。
注射件有利地在水平面(xy)中以相同的旋转方向取向并有利地位于塔底的液体部分中。
图3A示出在装备(1)的圆柱形部分(11)中的多个注射件(6)的使用，图3B示出在装备(1)的截锥形部分(12)中的多个注射件(5)的使用。
根据用于进入圆柱形部分(11)的注射件(6)的平面(xy)中的水平层(8)和根据用于进入截锥形部分(12)的注射件(5)的水平层(7)进行将注射件布置至装备壁中。在截锥形部分(12)中的注射件的层(7)和在圆柱形部分(11)中的注射件的层(8)分别包括在(z)轴上位于同样高度的数目为N个的注射件(5)或(6)。在图3中，N等于2。各层通过高度H分开。在一个层中，各注射件在平面(xy)中以等于360/N的角度δ与接下来的注射件分开。如图3中所示，注射件层可以在平面(xy)中相对于另一注射件层以角度γ偏移。
在截锥形或圆柱形部分的每一个中的层数目有利地为1至20个，优选1至10个并优选1至6个。
注入横向注射管(5)和(6)中的液体的速度V有利地为0.05 m.s-1至40 m.s-1，优选0.1 m.s-1至30 m.s-1，并非常优选0.5 m.s-1至10 m.s-1。优选地，注射管的直径根据注入的液体的流速设定尺寸从而获得期望的注射速度。
通过再循环管(4)再循环的液体的流速加上通过管(10)注入的液体的流速相对于在装备(1)中循环的含烃液体(2)的流速有利地为1%至400%，优选5%至100%，非常优选10%至60%，还更优选20至50%。
装备(1)的圆柱形部分(11)的直径D1有利地为0.1 m至30 m，优选0.5 m至20 m，非常优选1 m至10 m。
圆柱形部分(11)的直径D1与截锥形部分底部的出口管(9)的直径D2之间的比率(D1/D2)有利地为1.1至1000，优选2至500并优选3至100。
角度α为相对于圆柱形部分的垂直壁（z轴）的截锥形部分的倾斜角，并有利地为5°至85°，优选10至70°，非常优选15至60°，还更优选30至50°。
分别相对于截锥形部分的壁和圆柱形部分的壁的角度β1和θ1为5°至175°，优选10°至150°，非常优选15°至120°，更优选15°至90°，还更优选20°至60°。
相对于沿着圆柱形部分的y轴的直径的角度β2和θ2为90°至270°，优选90°至180°。非常优选地，角度β2和θ2等于90°。
通过装备壁进入圆柱形部分(11)中的各水平层(8)和进入截锥形部分(12)中的各水平层(7)的注射件数目N为1至30个，优选2至20个，非常优选2至10个，最优选2至6个。各层，无论是在同一个部分中还是在两个部分中，都能够具有不同数目的注射件N。
两层之间的高度H有利地为0.01 m至10 m，优选0.05 m至5 m，并非常优选0.1 m至1 m。
分开同一层的外周的注射件的角度δ为0°至180°，优选5°至120°，非常优选10°至90°。有利地，角度δ等于360/N，其中N表示每层的注射件的数目。
角度γ是指一层相对于另一层的角度偏移。这个角度可以为0°至180°，优选5°至120°，非常优选10°至90°。
实施例
使用BarracudaTM软件进行无注射件的具有锥形底部的装备（对比例）和包括根据本发明的具有再循环液体的横向注射件的设备的相同的具有锥形底部的装备中的液体/颗粒流体的计算流体动力学(CFD)机械模拟。这个软件使用用于流体相的Eulerian方法和用于微粒相的pseudo-Lagrangian方法（参见公开D.M. Snider, An Incompressible Three- Dimensional Multiphase Particle-in-Cell Model for Dense Particle Flows, Journal of Computational Physics 170 (2001), 523–549)）。
表1示出模拟条件和包括根据本发明的设备的装备的特征和尺寸（注射件数目、层数、注射件角度）。
Figure 829046DEST_PATH_IMAGE002
图4（4A：等距视图，4B：顶视图）示出没有注射件的构型（对比例），—其中固相的体积分数大于0.1体积%的装备的部分。这些区域代表积累了固体颗粒的区域。
图5（顶视图）示出根据本发明的具有注射件的构型，—其中固相的体积分数大于0.1体积%的装备的部分。
通过比较图4B和图5，由于使用液体的横向注射件和根据本发明的设备观察到积累固体区域的减少。按体积计算，发现在根据本发明的构型中，采用含烃液体的30%的再循环比，所述含烃液体用于供应两个进入截锥形部分中的注射件和两个进入具有根据本发明的几何结构的圆柱形部分中的注射件，上文定义的积累区域的数目被除以30。

Claims (36)

1.一种在装备(1)底部用于包含固体颗粒的含烃液体下降流的设备，装备(1)包括直径为D1的圆柱形上部(11)、具有相对于所述圆柱形上部的垂直轴(z)为5°至85°的倾斜角α的截锥形下部(12)和直径为D2的出口管(9)，特征在于所述设备包括：
至少一个使再循环的和/或补充的液体进入装备(1)的截锥形下部(12)中的注射件(5)；
至少一个使再循环的和/或补充的液体进入装备(1)的圆柱形上部(11)中的注射件(6)；
位于所述截锥形下部中的一个或多个所述注射件(5)相对于截锥形下部的壁在垂直面(xz)中以角度β1倾斜并在水平面(xy)中以角度β2倾斜；位于所述圆柱形上部中的一个或多个所述注射件(6)相对于所述圆柱形上部的壁在垂直面(xz)中以角度θ1倾斜并在水平面(xy)中以角度θ2倾斜，角度β1和θ1为5°至175°，角度β2和θ2为90°至270°。
2.根据权利要求1所述的设备，其包括用于再循环离开所述出口管(9)的一部分液体的再循环管(4)，所述再循环管(4)供应再循环液体至所述注射件(5)或(6)的至少一个。
3.根据权利要求1或2所述的设备，其包括供应补充液体至所述注射件(5)或(6)的至少一个的补充管(10)。
4.根据权利要求1或2的设备，其中所述注射件分别通过截锥形下部中的水平层(7)和通过圆柱形上部中的水平层(8)分配。
5.根据权利要求1或2的设备，其中圆柱形上部的直径D1和截锥形下部底部的出口管的直径D2之间的比率(D1/D2)为1.1至1000。
6.根据权利要求5的设备，其中所述比率为2至500。
7.根据权利要求6的设备，其中所述比率为3至100。
8.根据权利要求1或2的设备，其中角度α为10°至70°。
9.根据权利要求8的设备，其中角度α为15°至60°。
10.根据权利要求9的设备，其中角度α为30°至50°。
11.根据权利要求1或2的设备，其中分别相对于截锥形下部的壁和圆柱形上部的壁的角度β1和θ1为10°至150°。
12.根据权利要求11的设备，其中角度β1和θ1为15°至120°。
13.根据权利要求12的设备，其中角度β1和θ1为15°至90°。
14.根据权利要求13的设备，其中角度β1和θ1为20°至60°。
15.根据权利要求1或2的设备，其中相对于沿着圆柱形上部的y轴的直径的角度β2和θ2为90°至180°。
16.根据权利要求15所述的设备，其中角度β2和θ2等于90°。
17.根据权利要求1或2所述的设备，其中直径D1为0.1 m至30 m。
18.根据权利要求17所述的设备，其中直径D1为0.5 m至20 m。
19.根据权利要求18所述的设备，其中直径D1为1 m至10 m。
20.根据权利要求4所述的设备，其中两个水平层之间的高度H为0.01 m至10 m。
21.根据权利要求20所述的设备，其中两个水平层之间的高度H为0.05 m至5 m。
22.根据权利要求21所述的设备，其中两个水平层之间的高度H为0.1 m至1 m。
23.根据权利要求4所述的设备，其中每层的注射件的数目N为1至30个。
24.根据权利要求23所述的设备，其中每层注射件的数目为2至20个，同一层内的所述注射件以等于360/N的角度δ间隔开，其中N表示每层的注射件数目。
25.根据权利要求24所述的设备，其中每层的注射件的数目为2至10个。
26.根据权利要求25所述的设备，其中每层的注射件的数目为2至6个。
27.根据权利要求1或2所述的设备，其中所述装备为能够处理含烃原料的用于分离气体/液体的装置。
28.通过使用根据权利要求1至27之一的设备转化含烃原料的方法。
29.根据权利要求28所述的方法，其在用于含烃级分的原料的沸腾床中用于实施加氢转化步骤，所述烃级分的至少50重量%具有高于300℃的沸点。
30.根据权利要求28或29所述的方法，其中注入所述注射件中的液体的速度V为0.05 m·s-1至40 m · s-1。
31.根据权利要求30所述的方法，其中注入所述注射件中的液体的速度V为0.1 m · s-1至30 m · s-1。
32.根据权利要求31所述的方法，其中注入所述注射件中的液体的速度V为0.5 m · s-1至10 m · s-1。
33.根据权利要求28或29所述的方法，其中再循环的和/或补充的液体相对于在装备中循环的含烃液体的注射率为1%至400%。
34.根据权利要求33所述的方法，其中所述注射率为5%至100%。
35.根据权利要求34所述的方法，其中所述注射率为10%至60%。
36.根据权利要求35所述的方法，其中所述注射率为20至50%。
CN201811189527.8A 2017-10-13 2018-10-12 用于限制固体沉积在具有锥形底部的装备中的现象的包括液体的横向注射件的设备 Active CN109663547B (zh)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR1759606A FR3072302B1 (fr) 2017-10-13 2017-10-13 Dispositif comprenant des injections laterales de liquide pour limiter les phenomenes de depots solides dans les equipements a fond conique
FR1759606 2017-10-13

Publications (2)

Publication Number Publication Date
CN109663547A CN109663547A (zh) 2019-04-23
CN109663547B true CN109663547B (zh) 2022-07-08

Family

ID=61003125

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201811189527.8A Active CN109663547B (zh) 2017-10-13 2018-10-12 用于限制固体沉积在具有锥形底部的装备中的现象的包括液体的横向注射件的设备

Country Status (7)

Country Link
US (2) US20190112536A1 (zh)
EP (1) EP3470137B1 (zh)
CN (1) CN109663547B (zh)
BR (1) BR102018070766B1 (zh)
FR (1) FR3072302B1 (zh)
MX (1) MX2018012355A (zh)
RU (1) RU2771035C2 (zh)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3831472A1 (en) * 2019-12-03 2021-06-09 Basell Polyolefine GmbH High-pressure polymerization system and high-pressure polymerization process for the polymerization of ethylenically unsaturated monomers

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3846079A (en) * 1970-05-19 1974-11-05 Inst Francais Du Petrole Vertical reaction vessel for effecting reaction of liquid and gaseous reactants by liquid-gas contact
US4146359A (en) * 1976-06-25 1979-03-27 Occidental Petroleum Corporation Method for reacting nongaseous material with a gaseous reactant
US6238912B1 (en) * 1995-07-15 2001-05-29 Philip Coley Moore Method and apparatus for contacting gas and liquid
CN202654922U (zh) * 2012-04-10 2013-01-09 河北国惠环保科技有限公司 一种防止塔底固体悬浮物沉积的烟气脱硫塔
WO2014117725A1 (en) * 2013-01-31 2014-08-07 Shanghai Advanced Research Institute, Chinese Academy Of Sciences Slurry-bed reactor and method of use thereof
CN106841661A (zh) * 2017-01-12 2017-06-13 中国科学院工程热物理研究所 一种示踪粒子发生器

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS538721B2 (zh) * 1972-04-07 1978-03-31
US4615792A (en) * 1985-04-25 1986-10-07 Uop Inc. Hydrogen circulation for moving bed catalyst transfer systems
US10188119B2 (en) * 2001-07-16 2019-01-29 Foret Plasma Labs, Llc Method for treating a substance with wave energy from plasma and an electrical arc
US7416571B2 (en) * 2005-03-09 2008-08-26 Conocophillips Company Compact mixer for the mixing of gaseous hydrocarbon and gaseous oxidants
US9382359B2 (en) * 2012-08-29 2016-07-05 Borealis Ag Reactor assembly and method for polymerization of olefins
KR102259574B1 (ko) * 2013-11-29 2021-06-02 사우디 베이식 인더스트리즈 코포레이션 반응기에서 올레핀 단량체의 연속 중합 방법
EP3074433B1 (en) * 2013-11-29 2018-05-23 Saudi Basic Industries Corporation Process for continuous polymerization of olefin monomers in a reactor
CN105916890B (zh) * 2013-11-29 2019-02-22 沙特基础工业公司 用于α-烯烃单体的连续聚合的多区段反应器
US10596492B2 (en) * 2014-07-09 2020-03-24 Sudhin Biopharma Particle settling devices
US20190210042A1 (en) * 2014-07-09 2019-07-11 Sudhin Biopharma Particle setting devices
CA2987851A1 (en) * 2015-06-01 2016-12-08 Cetamax Ventures Ltd. Systems and methods for processing fluids
EP3331924B1 (en) * 2015-08-07 2019-08-21 SABIC Global Technologies B.V. Process for the polymerization of olefins
EP3497052A4 (en) * 2016-08-15 2020-03-25 Advanced Energy Materials, LLC FLAME-BASED FLUIDIZED BED REACTOR FOR THE PRODUCTION OF NANOMATERIALS

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3846079A (en) * 1970-05-19 1974-11-05 Inst Francais Du Petrole Vertical reaction vessel for effecting reaction of liquid and gaseous reactants by liquid-gas contact
US4146359A (en) * 1976-06-25 1979-03-27 Occidental Petroleum Corporation Method for reacting nongaseous material with a gaseous reactant
US6238912B1 (en) * 1995-07-15 2001-05-29 Philip Coley Moore Method and apparatus for contacting gas and liquid
CN202654922U (zh) * 2012-04-10 2013-01-09 河北国惠环保科技有限公司 一种防止塔底固体悬浮物沉积的烟气脱硫塔
WO2014117725A1 (en) * 2013-01-31 2014-08-07 Shanghai Advanced Research Institute, Chinese Academy Of Sciences Slurry-bed reactor and method of use thereof
CN106841661A (zh) * 2017-01-12 2017-06-13 中国科学院工程热物理研究所 一种示踪粒子发生器

Also Published As

Publication number Publication date
MX2018012355A (es) 2019-06-24
EP3470137B1 (fr) 2024-04-10
RU2771035C2 (ru) 2022-04-25
BR102018070766B1 (pt) 2022-12-13
EP3470137A1 (fr) 2019-04-17
FR3072302A1 (fr) 2019-04-19
RU2018135293A (ru) 2020-04-08
US20210095214A1 (en) 2021-04-01
CN109663547A (zh) 2019-04-23
US20190112536A1 (en) 2019-04-18
FR3072302B1 (fr) 2022-04-01
BR102018070766A2 (pt) 2019-09-17
US11549074B2 (en) 2023-01-10
RU2018135293A3 (zh) 2021-11-22

Similar Documents

Publication Publication Date Title
JP7126443B2 (ja) 適時原料を用いる改良型沸騰床リアクター
EP3020788B1 (en) Ebullated-bed process for feedstock containing dissolved hydrogen
EP1169412B1 (en) Rapid thermal processing of bitumen feedstocks
EP2782977B1 (en) Slurry bed hydroprocessing and system
JP7126442B2 (ja) プラスチック二次加工製品の生産速度が上昇した改良型沸騰床リアクター
TW201602331A (zh) 整合選擇性串聯脫瀝青及回收已脫瀝青餾份之用於重烴進料轉化的方法
CN114402056A (zh) 具有改进的液/气分离的用于固定床加氢裂化和沸腾床加氢转化的集成方法
CN109663547B (zh) 用于限制固体沉积在具有锥形底部的装备中的现象的包括液体的横向注射件的设备
CN110496423B (zh) 用于限制旋涡和固体沉积物的装置
CN111534331B (zh) 带有液体的横向注入器以限制淤塞的包括具有减小的截面和可变倾斜角的底部的容器
CN111804245B (zh) 包括具有逐渐减小的截面和变化的倾斜角的再循环杯的三相反应器
JP7446081B2 (ja) 真空ボトム中にアスファルテンの再利用蓄積のないアップグレードされた沸騰床式反応器
FI3470137T3 (zh)
US11084991B2 (en) Two-phase moving bed reactor utilizing hydrogen-enriched feed

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant