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WO2016176983A1 - Procédé de régulation de température de procédé d'hydrogénation ainsi que procédé de conception s'y rapportant et utilisation de ces derniers - Google Patents

Procédé de régulation de température de procédé d'hydrogénation ainsi que procédé de conception s'y rapportant et utilisation de ces derniers Download PDF

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WO2016176983A1
WO2016176983A1 PCT/CN2015/095205 CN2015095205W WO2016176983A1 WO 2016176983 A1 WO2016176983 A1 WO 2016176983A1 CN 2015095205 W CN2015095205 W CN 2015095205W WO 2016176983 A1 WO2016176983 A1 WO 2016176983A1
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Prior art keywords
temperature
reactor
separator
stage
hydrogen
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Ceased
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PCT/CN2015/095205
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English (en)
Chinese (zh)
Inventor
李苏安
邓清宇
王坤朋
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Catech Technology Co Ltd
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Catech Technology Co Ltd
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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
    • 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
    • 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
    • C10G65/14—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural parallel stages only
    • C10G65/18—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural parallel stages only including only cracking steps
    • G—PHYSICS
    • G05—CONTROLLING; REGULATING
    • G05D—SYSTEMS FOR CONTROLLING OR REGULATING NON-ELECTRIC VARIABLES
    • G05D23/00—Control of temperature
    • G05D23/19—Control of temperature characterised by the use of electric means
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/107—Atmospheric residues having a boiling point of at least about 538 °C
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1077—Vacuum residues

Definitions

  • the invention relates to a multi-optimized temperature control method for a slurry bed hydrogenation device and a design method and application thereof.
  • the hydrogenation device comprises a slurry bed hydrogenation reactor and a separation system, and belongs to the fields of petrochemical and coal chemical industry.
  • the essence of the hydrocracking reaction process is high temperature, high pressure, hydrogen and strong exothermic catalytic hydrogenation. If the operation is improper, the flying temperature is easy to occur.
  • the flying temperature means that the reactor is in an unstable operating state, when the operating parameters With small disturbances, the temperature in the local part of the reactor or in the entire reactor rises sharply and is out of control. If the temperature of the reactor exceeds 860 ° C, it will cause the catalyst to be deactivated or the internal components of the reactor will be damaged, which will lead to damage to the reactor wall and even a vicious accident of fire and explosion.
  • the present invention proposes an effective temperature control method for a slurry bed reactor and a separation system in a slurry bed reaction apparatus.
  • the invention provides a multi-optimized temperature control method for a slurry bed hydrogenation device, in which a cooling medium is driven into a pipeline between the reactors at various stages, so that the coolant and the reaction material are thoroughly mixed in the pipeline to form a uniform medium and then enter The next stage of the reactor, thereby reducing the temperature inside the reactor.
  • a multi-optimized temperature control method for a hydrogenation unit in which a coolant is injected into a pipeline before a certain stage or multi-stage reactor inlet, the coolant being delivered through at least one cooling line and the flow rate being controllable.
  • the method also includes injecting a coolant into a conduit on a certain or multi-stage separator and/or a pre- or multi-stage separator inlet.
  • the coolant comprises cold hydrogen or cold oil or a mixture of the two, the cold hydrogen is recycled hydrogen, the purity is 85 vol% or more, and the temperature is 30-250 ° C; the cold oil is in the slurry bed reactor
  • the circulating heavy oil produced has a temperature of 50-450 °C.
  • the cooling pipelines are 1-8, and each pipeline is provided with a temperature self-control valve and/or a hand valve and a temperature sensor.
  • the number of reactor stages is 2-3, and the number of stages of the separator is 2-6.
  • the temperature before the inlet of the first stage reactor is controlled at 350-465 ° C, and the temperature between the first and second reactors is controlled at 380-480. °C, the temperature between the second and third reactors is controlled at 360-480 °C, the operating temperature of the high temperature and high pressure separator is controlled at 300-470 °C, the operating pressure is 17-22 MPa, and the reactor outlet material is shut off.
  • the residence time is 0.5-60 minutes, and the subsequent separator operating temperature and operating pressure do not exceed the operating temperature and pressure of the high temperature and high pressure separator, and the residence time is 0.5-60 minutes.
  • the reaction hydrogen is divided into two ways of heating, one way is heated in a hydrogen heating furnace, and all the way is mixed with the raw materials and then heated in the raw material heating furnace; then the hydrogen gas at the outlet of the hydrogen heating furnace is mixed with the reaction hydrogen and the raw materials.
  • the slurry enters the first-stage reactor, and is mixed with the stream of the first-stage reactor outlet to enter the secondary reactor, and is mixed with the stream of the secondary reactor outlet to enter the third-stage reactor.
  • the reactor all the way into the high temperature and high pressure separator.
  • An optimized temperature controlled slurry bed hydrogenation apparatus wherein at least one cooling line is connected to a pipeline and/or a separator before a reactor of a certain stage or multiple stages and a separator inlet, in the cooling pipeline
  • the coolant is cold hydrogen or cold oil or a mixture of the two, the amount of which is controllable.
  • a multi-optimized temperature control method for a slurry bed hydroprocessing device for a heavy oil hydrogenation process, a coal direct liquefaction process, and a reactor and separator in a coal-oil mixing process the heavy oil including heavy One or more combinations of crude oil, residual oil, catalytic oil slurry, deoiled asphalt, coal tar, the coal includes one or more combinations of lignite, bituminous coal, non-stick coal, and the oil-coal mixing process
  • the ratio of medium oil to coal ranges from 97:3 to 30:70.
  • a multi-optimized temperature control design method for slurry bed hydrogenation equipment in which a coolant is injected into a hydrogenation equipment to control temperature, and the injection position is respectively located in a pipeline before the inlet of a certain stage or multi-stage reactor, a certain stage or multiple stages of separation
  • the coolant is delivered through at least one cooling line and the flow is controllable.
  • a multi-optimized temperature control method for a slurry bed hydrogenation apparatus of the present invention in order to control the reactor temperature and maintain the stability of the reaction state in the reactor, a coolant is injected into the pipeline between the inlets of the reactor, so that the coolant The outlet material of the upper reactor is thoroughly mixed in the pipeline and then enters the next-stage reactor. Since the temperature of the reaction material is lowered, the temperature of the next-stage reactor is controlled within a reasonable range, and the reaction system in the reactor is ensured. Uniform density to avoid the formation of vortex flow.
  • the temperature control method of the present invention when the temperature of a certain stage reactor or multi-stage reactor rises, the coolant is introduced into the pipeline before the corresponding reactor inlet, and multiple cooling is designed for each injection position.
  • the flow rate of each pipeline can be adjusted. According to the difference between the target temperature and the reactor temperature, the flow rate is adjusted to control the reactor to be in a safe temperature range. Therefore, the temperature control method of the invention is simple in operation, easy to implement in engineering implementation, prevents the formation of the separator from flying temperature and vortex flow, and greatly improves the operational stability of the hydrogenation equipment.
  • the temperature control method of the present invention further comprises introducing a coolant into the slurry bed separation system to control the temperature of the separator to minimize the polycondensation reaction in the separator, minimizing the possibility of coking, and improving liquid and solid. Separation efficiency, thereby increasing liquid yield and circulating hydrogen purity.
  • Circulating hydrogen or circulating heavy oil is an intermediate product of heavy oil hydrogenation, which is easy to obtain, low in cost, and also a reactant of hydrogenation reaction. It does not produce by-products in the reactor, and may occur as the reactants in the original reaction system. The reaction is also consistent, and does not change the operating parameters of the original reaction system, so that the stability of the entire hydrogenation system is easy to control.
  • a temperature control valve or a hand valve and a temperature sensor are arranged on each cooling pipe to improve the operability and safety of the temperature control and to facilitate automatic control.
  • the slurry bed hydrogenation system includes a 2-3 stage reactor and a 2-6 stage separator to achieve sufficient hydrogenation and separation to obtain more liquid oil.
  • the method is particularly suitable for use in the reactor stage, and the reaction heat of the reactant of the upper stage can be fully utilized reasonably to achieve efficient use of heat while ensuring the stability of the next stage reactor. Since the reaction does not occur in the separator and is relatively stable, the method can be directly applied to the separator to quickly achieve the cooling effect.
  • the temperature can be controlled by injecting the coolant, or the temperature can be controlled by setting two channels of hydrogen separately heating and remixing.
  • one way of hydrogen is separately heated to a higher temperature and mixed with a lower temperature mixture of the raw material heating furnace outlet, and the temperature of the primary reactor inlet is adjusted by controlling the mixing ratio; on the other hand, the higher temperature hydrogen is separately It is introduced into the inlet of the second-stage or third-stage reactor and the inlet of the high-temperature high-pressure separator to increase the partial pressure of hydrogen in the secondary or tertiary reactor and the separator, thereby solving the reaction of the multi-stage reactor due to insufficient hydrogen partial pressure. Insufficient problems and the problem that the separator has a polycondensation reaction due to high temperature and low partial pressure of hydrogen.
  • the method is particularly suitable for a slurry bed reactor and a separation system in a heavy oil hydrogenation process, a coal direct liquefaction process and a coal-oil mixing process which have a large solid content and cannot achieve temperature uniform control by the existing temperature control method.
  • the hydrocracking reaction in the slurry bed reactor is a strong exothermic reaction and has strict requirements on the reaction temperature, it is necessary to accurately determine the reaction progress, heat release and temperature rise under different working conditions when designing the reactor. Calculations stabilize the operating temperature of the reactor by controlling the inlet temperature of the reactor.
  • the slurry bed separation system is directly connected to the outlet of the reactor, and the temperature is high, and side reactions are likely to occur, which affects the separation effect. Therefore, the method fully considers the reaction characteristics of the slurry bed reactor and the separator, and efficiently controls the temperature in the slurry bed reactor and the separator to ensure long-term stable operation of the hydrogenation equipment and avoid safety accidents.
  • FIG. 1 is a schematic view showing a slurry bed hydrogenation and a reaction scheme according to an embodiment of the present invention
  • FIG. 2 is a schematic view showing a temperature control method of a slurry bed reactor according to an embodiment of the present invention
  • FIG. 3 is a schematic diagram of a temperature control method of a separation system 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-raw material; 10-hot high-scoring gas; 11-cold oil; 12-cold hydrogen; 13- Reaction product; 14-high temperature low pressure separator; 15-intermediate low pressure separator; 16-normal temperature and pressure separator; 17-medium temperature high pressure separator; 18-normal temperature high pressure separator; 19-demineralized water; 20-tail gas; Normal temperature oil; 22-waste water; 23-medium temperature oil; 24-high temperature oil.
  • This embodiment is a temperature control method for a slurry bed hydrogenation equipment involved in the oil coal mixing process, the hydrogenation reactor is a second stage, and the separator is 6 stages.
  • the specific temperature control process is as follows:
  • the hydrogenation and reaction process of the slurry bed reactor of the embodiment of the present invention firstly supplements the hydrogen gas 7 with the circulating hydrogen gas 8, and then the gas with the high temperature and high pressure separator 6 is the hot high gas 10 in the hydrogen gas.
  • the heat exchange at the high gas heat exchanger 1 is raised to 425 ° C hydrogen.
  • 20% of the hydrogen is mixed with the coal slurry feed 9, 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 ° C of high temperature hydrogen.
  • the high-temperature hydrogen is divided into three-way transportation: a part of the mixture and the mixture flow, the control feed temperature is 385 ° C, and the hydrogenation reaction occurs in the first-stage reactor 4; a part is mixed with the first-stage reactor outlet material and then enters the secondary reactor 5 to further occur.
  • the hydrogen feed is 1/15 of the hydrogen feed of the first reactor; a portion enters the high temperature and high pressure separator 6 from the bottom.
  • FIG. 2 is a schematic diagram of a temperature control method of a slurry bed reactor according to an embodiment of the present invention.
  • the temperature sensor detects that the reaction temperature of the secondary reactor 5 rises above a normal temperature range, it is to the first and second levels.
  • the coolant is introduced into the pipeline between the reactors, and the cooling medium includes the circulating heavy oil produced in the oil-coal mixing process, the cold oil 11, the temperature is 225 ° C, two cooling pipes, and the circulating hydrogen - cold hydrogen 12, the purity is 95.5 vol%, the temperature is 55 ° C, delivered through 4 cooling lines, the flow rate is controlled by the automatic valve (supplement flow data) until the temperature in the secondary reactor is controlled within the range of 410-420 ° C, the valve is closed, and the valve is stopped. Inject coolant.
  • the reaction product 13 flowing out from the outlet of the secondary reactor enters the high-temperature high-pressure separator 6, the operating temperature is 420 ° C, and the operating pressure is 18.7 MPa.
  • the cold oil 11 is driven by the temperature sensor.
  • the flow rate of the cold hydrogen 12 stabilizes the temperature of the high-temperature high-pressure separator 6 at about 420 ° C.
  • the gas phase separated from the upper portion of the high-temperature high-pressure separator 6 is cooled, and then enters the intermediate-temperature high-pressure separator 17 .
  • the liquid level control valve After the liquid level control valve is adjusted, it enters the high temperature and low pressure separator 14; the operating temperature of the medium temperature high pressure separator 17 is 285 ° C, the operating pressure is 18.6 MPa, and the gas phase separated from the upper portion enters the normal temperature high pressure separator after cooling, water injection and secondary cooling.
  • the liquid phase is adjusted by the liquid level control valve and enters the medium temperature low pressure separator 15; the normal temperature high pressure separator 18 operates at a temperature of 55 ° C, the operating pressure is 18.5 MPa, and the gas phase separated from the upper portion is used as the circulating hydrogen 8 , and the normal temperature high pressure separator 18
  • the lower liquid phase is adjusted by the liquid level control valve to enter the normal temperature low pressure separator 16; the high temperature low pressure separator 14 operating temperature is 420 ° C, the operating pressure is 3.0 MPa, in order to operate
  • the temperature is kept constant, and the flow rate of the cold oil 11 or the cold hydrogen 12 that is driven therein by the temperature sensor is controlled to stabilize the temperature of the high-temperature low-pressure separator 14.
  • the gas phase separated from the upper part is cooled and then enters the medium-temperature low-pressure separator 15.
  • the liquid phase is adjusted by the liquid level control valve as a high-temperature oil 24 separator; the medium-temperature low-pressure separator 15 operating temperature It is 285 ° C, the operating pressure is 2.9 MPa, the upper gas phase is cooled and then enters the normal temperature low pressure separator 16 , the liquid phase is adjusted by the liquid level control valve as a medium temperature oil 23 out separator; the normal temperature low pressure separator operating temperature is 55 ° C, operation
  • the pressure is 2.8 MPa, the upper gas phase is used as a tail gas 20 separator to enter the gas treatment device, and the lower liquid phase is used as a room temperature oil 21 separator, and the liquid collection bag contains ammonium bicarbonate and ammonium sulfide wastewater 22 to the wastewater treatment device.
  • the temperature stability of the first-stage reactor 4 and the uniformity of the reactants are ensured in the actual operation, and the temperature in the secondary reactor 5, the reactant and hydrogen partial pressure, and the hydrogen content in the high-temperature high-pressure separator 6 are ensured.
  • the pressure also remained stable and no coking occurred.
  • a method of introducing a coolant into the pipeline before the inlet of the primary reactor 4 may be employed, but the controlled hydrogen heating of the present embodiment is employed.
  • the method of controlling the inlet temperature of the primary reactor is a more preferred mode. If the number of reactor stages is three, the temperature control method of the three-stage reactor is the same as the temperature control method of the above two-stage reactor.
  • using the multi-optimized slurry bed reaction equipment temperature control method of the present invention can ensure uniform temperature throughout the reactors at all stages, so that the entire reaction system is in a stable state;
  • the operating temperature of the separator makes the separation system under a steady state operating condition, and for the gas phase, the purpose of reducing the operating pressure of the downstream device and ensuring the purity of the circulating hydrogen is achieved. It is to ensure the liquid yield and the separation effect is optimal.
  • the coolant used is recycled hydrogen and recycled heavy oil, which is the reaction intermediate and also the reaction raw material.
  • the advantages of this are: (1) circulating hydrogen and recycled heavy oil are easily obtained; (2) no by-products are produced; The system operating parameters change little, so that the system is in a controllable state; (4) the use of two sources of media to control the temperature is more secure.

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

Abstract

L'invention porte sur un procédé de régulation de température de procédé d'hydrogénation ainsi que sur un procédé de conception s'y rapportant et sur une utilisation de ces derniers. Le procédé de régulation de température de procédé d'hydrogénation consiste à injecter un fluide de refroidissement dans un dispositif d'hydrogénation afin de réguler la température, des positions d'injection étant respectivement situées au niveau d'un tuyau à l'avant d'un réacteur comportant un certain nombre d'étages ou de multiples étages, dans un tuyau à l'avant d'un séparateur comportant un certain nombre d'étages ou de multiples étages et/ou sur le séparateur comportant un certain nombre d'étages ou de multiples étages. Le liquide de refroidissement est transporté par le biais d'au moins un tuyau de refroidissement et l'écoulement peut être régulé. Le procédé de régulation de température empêche de manière efficace un emballement de température de réacteur et la formation de flux tourbillonnaires et empêche également l'apparition du phénomène de cokéfaction à l'intérieur du séparateur, ce qui permet d'améliorer la stabilité fonctionnelle du dispositif d'hydrogénation.
PCT/CN2015/095205 2015-05-07 2015-11-20 Procédé de régulation de température de procédé d'hydrogénation ainsi que procédé de conception s'y rapportant et utilisation de ces derniers Ceased WO2016176983A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
CN201510229692.1A CN104888666A (zh) 2015-05-07 2015-05-07 一种浆态床反应器控温方法及其设计方法和用途
CN201510229692.1 2015-05-07
CN201510780561.2 2015-11-13
CN201510780561.2A CN105441128B (zh) 2015-05-07 2015-11-13 一种加氢工艺的控温方法及其设计方法和用途

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CN115200389A (zh) * 2022-08-11 2022-10-18 镇海石化建安工程股份有限公司 一种加氢换热组件及具有该组件的加氢换热系统
CN116020374A (zh) * 2023-01-19 2023-04-28 中国石化工程建设有限公司 一种乙炔加氢反应装置及其飞温控制方法
CN116726806A (zh) * 2023-07-20 2023-09-12 濮阳市联众兴业化工有限公司 一种粗醇气相加氢反应器

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CN105273747B (zh) * 2015-11-18 2017-05-03 北京中科诚毅科技发展有限公司 一种浆态床加氢反应器的控温措施及其设计方法和用途
CN108531217A (zh) * 2017-03-01 2018-09-14 何巨堂 导液降温式碳氢料加氢反应器三相产物的分离方法
CN110591763B (zh) * 2019-09-10 2021-01-15 南京延长反应技术研究院有限公司 一种煤间接液化的智能强化控制系统及工艺

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