WO2020186634A1 - 一种微界面强化加氢反应*** - Google Patents

一种微界面强化加氢反应*** Download PDF

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WO2020186634A1
WO2020186634A1 PCT/CN2019/090268 CN2019090268W WO2020186634A1 WO 2020186634 A1 WO2020186634 A1 WO 2020186634A1 CN 2019090268 W CN2019090268 W CN 2019090268W WO 2020186634 A1 WO2020186634 A1 WO 2020186634A1
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micro
reaction
hydrogenation reaction
liquid
interface
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PCT/CN2019/090268
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English (en)
French (fr)
Inventor
张志炳
周政
张锋
李磊
孟为民
王宝荣
杨高东
罗华勋
杨国强
田洪舟
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南京延长反应技术研究院有限公司
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Priority to DE212019000177.7U priority Critical patent/DE212019000177U1/de
Application filed by 南京延长反应技术研究院有限公司 filed Critical 南京延长反应技术研究院有限公司
Priority to RU2020129854U priority patent/RU207190U1/ru
Priority to JP2020600106U priority patent/JP3231870U/ja
Publication of WO2020186634A1 publication Critical patent/WO2020186634A1/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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0093—Microreactors, e.g. miniaturised or microfabricated reactors
    • 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
    • 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
    • B01J19/0053—Details of the reactor
    • 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
    • B01J19/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J19/087—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy
    • 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
    • B01J19/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J19/10—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing sonic or ultrasonic vibrations
    • 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
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B01J4/002—Nozzle-type elements
    • 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
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B01J4/004—Sparger-type elements
    • 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
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • 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
    • 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
    • C10G45/04—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 characterised by the catalyst used
    • C10G45/06—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 characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
    • C10G45/08—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 characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
    • 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
    • B01J2208/00823—Mixing elements
    • 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
    • B01J2208/00902—Nozzle-type feeding elements
    • 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
    • B01J2208/00911—Sparger-type feeding elements
    • 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
    • B01J2208/00938—Flow distribution elements

Definitions

  • the invention belongs to the technical field of reaction strengthening, and specifically relates to a micro-interface strengthening hydrogenation reaction system.
  • Gas-liquid, gas-liquid-solid and other gas-liquid reaction processes are widely present in the fields of energy, petrochemical, and fine chemicals.
  • gas-liquid multiphase reactions such as oxidation, hydrogenation, and chlorination
  • the macroscopic reaction rate is generally restricted by the mass transfer process.
  • the volumetric mass transfer coefficient of the gas-liquid reaction is mainly affected by the mass transfer coefficient and the area of the gas-liquid phase boundary. Studies have shown that the phase boundary area has a greater influence on the volumetric mass transfer coefficient and is easy to control. Therefore, increasing the phase boundary area is regarded as an effective way to increase the gas-liquid macroscopic reaction rate.
  • Bubbling reactors and stirred-bubbling reactors are currently commonly used gas-liquid reactors.
  • the bubble diameter is usually larger than 3mm, or even centimeter level, and its mass transfer interface area is limited.
  • the turbulence of the liquid must be promoted by increasing the amount of air blown, so that the bursting of the bubbles is intensified to increase the number of bubbles, and thus the interface area. This will inevitably reduce the gas utilization rate, increase the compressor power and exhaust emissions, and cause the transition of energy consumption, material loss and environmental pollution.
  • Stirring-bubbling gas-liquid reactors often form large vortices that affect the macroscopic movement of bubbles but have little effect on bubble breaking.
  • the bubbles cannot be broken effectively, so the diameter is too large and the mass transfer area is limited, resulting in low reaction efficiency.
  • tower bubbling reactors In order to strengthen gas-liquid mass transfer, tower bubbling reactors generally add trays, static mixers and other internals in the tower to enhance mixing, while stirring tanks need to install different structures of stirring blades or inner cylinders to increase The gas content of the liquid layer.
  • the bubble diameter is usually 3-30mm, and the phase boundary area and mass transfer coefficient (liquid side, gas side, solid-liquid) provided are limited, so it is difficult to achieve breakthrough improvement in reaction performance.
  • the present invention proposes a micro-interface strengthening hydrogenation reaction system, which aims to solve the problem of increasing the phase boundary area of each reaction phase by means of high temperature and high pressure in the existing hydrogenation reaction strengthening system during the reaction strengthening process. Furthermore, while increasing the mass transfer rate, it is easy to cause problems such as high energy consumption and production cost, high investment intensity, short equipment operation cycle, multiple failures, and poor intrinsic safety, which pose challenges to industrial mass production.
  • the present invention provides a micro-interface strengthening hydrogenation reaction system, which includes:
  • the main body of the reactor is used as a reaction chamber in the hydrogenation reaction process to ensure that the hydrogenation reaction can fully proceed;
  • Micro Interfacial Generator which is connected to the main body of the reactor, and is used for the hydrogen and liquid and/or solid-liquid mixture in the hydrogenation process to enter the main body of the reactor.
  • the hydrogen and/or liquid phase reactant was broken into micro bubbles and/or micro droplets with a diameter of micrometers in a predetermined action mode through mechanical microstructures and/or turbulent microstructures in the micro-interface generator , In order to increase the mass transfer area of the phase boundary between the hydrogen and the liquid and/or solid-liquid mixture during the reaction, improve the mass transfer efficiency between the reaction phases, and strengthen the mass transfer under the preset temperature and pressure conditions.
  • the reaction rate of hydrogenation is used for the hydrogen and liquid and/or solid-liquid mixture in the hydrogenation process to enter the main body of the reactor.
  • the preset mode of action is selected from one or more of the mode of microchannel action, the action of field force, and the action of mechanical energy;
  • the microchannel action mode is to construct the microstructure of the flow channel, so that the gas and/or liquid phase passing through the micro flow channel is broken into micro bubbles and/or micro droplets;
  • the field force action mode is to use external field force to input energy into the fluid in a non-contact manner to break it into the microbubbles or microdroplets;
  • the action mode of the mechanical energy is to use the mechanical energy of the fluid to convert it into the surface energy of bubbles or droplets, so that the bubbles or droplets are broken into the microbubbles or microdroplets.
  • the micro-channel action mode is selected from one or more of micro-porous aeration method, micro-nano-porous membrane method, micro-channel method and micro-fluidic method.
  • the field force action mode includes: pressure field action, supergravity field action, ultrasonic field action or electromagnetic wave field action.
  • the action mode of the mechanical energy includes: impinging stream breaking method, cyclotron shear breaking method, spray method or gas-liquid mixed flow pump method.
  • the reactor main body includes: a tank reactor, a tubular reactor, a tower reactor, a fixed bed reactor or a fluidized bed reactor.
  • the micro-interface generator is connected to the gas and/or liquid inlet end of the reactor body, and the number of the micro-interface generator is at least one set.
  • the preset pressure range is 10%-80% of the pressure required by the existing hydrogenation intensified reaction system.
  • the range of the micron level is greater than or equal to 1 ⁇ m and less than 1 mm.
  • the micro-interface intensified hydrogenation reaction system can be applied to chemical industry, metallurgy, bioengineering, petrochemical industry, medicine, environmental treatment, biochemical fermentation, oil refining, aquaculture, fine chemical industry , Biological fermentation and hydrogenation reactions in the field of mineral mining.
  • the beneficial effect of the present invention is that the micro-interface strengthening hydrogenation reaction system provided by the present invention, by connecting the micro-interface generator to the main body of the reactor, the hydrogen and liquid in the hydrogenation reaction process And/or the solid-liquid mixture material breaks the hydrogen and/or liquid phase reactants in the micro-interface generator through mechanical microstructures and/or turbulent microstructures in a predetermined action mode before entering the reactor body Micro-bubbles and/or micro-liquid droplets with a diameter of micrometers are formed, which effectively increases the mass transfer area of the phase boundary between the hydrogen and the liquid and/or solid-liquid mixture during the reaction process, and greatly improves the interaction between the reaction phases.
  • the mass transfer efficiency achieves the purpose of strengthening the reaction within the lower preset pressure range, while greatly reducing the energy consumption and production cost in the reaction process, reducing the investment intensity, extending the equipment operation cycle, and ensuring the reaction
  • the intrinsic safety of the process is poor, which effectively guarantees the industrialized mass production of reaction products.
  • different crushing methods can be selected according to the characteristics of different reaction phases and process requirements, such as microchannels, field forces or mechanical energy effects on the reaction medium.
  • the gas and/or liquid crushing effectively ensures the effectiveness of crushing the gas and/or liquid in the reaction medium before the reaction medium enters the main body of the reactor during the hydrogenation process, and ensures the gas, liquid and/or liquid phase and/or The mass transfer efficiency between the gas phase, the liquid phase and the solid phase further improves the reaction efficiency.
  • Figure 1 is a schematic structural diagram of a kettle-type micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention
  • FIG. 2 is a schematic structural diagram of a tubular micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention
  • Figure 3 is a schematic structural diagram of a tower-type micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention
  • FIG. 4 is a schematic structural diagram of a fixed bed micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention.
  • FIG. 5 is a schematic structural diagram of an emulsion bed micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention.
  • FIG. 6 is a schematic structural diagram of a suspended bed micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention.
  • Fig. 7 is a schematic structural diagram of a fluidized bed micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention.
  • the micro-interface strengthening hydrogenation reaction system includes: a reactor body 1 and a micro-interface generator (MIG) 2; wherein, the reactor body 1 is used for hydrogenation The reaction chamber during the reaction process to ensure that the hydrogenation reaction can fully proceed; the micro-interface generator 2 is connected to the reactor main body 1 for the hydrogen and liquid and/or liquid and/or Before the solid-liquid mixture material enters the reactor body, the hydrogen and/or liquid phase reactants are broken into diameters in the micro-interface generator through mechanical microstructures and/or turbulent microstructures in a preset mode of action.
  • MIG micro-interface generator
  • the mass transfer area of the phase boundary between the phase and the liquid phase and/or the solid phase greatly improves the mass transfer efficiency between the hydrogen and the reaction phases, and finally realizes the strengthening of the mass transfer area under the lower preset temperature and pressure conditions.
  • the purpose of the hydrogenation reaction is to effectively solve the problems of high temperature, high pressure, high material consumption, high investment, high safety risk, etc. in the traditional hydrogenation reaction process, thereby significantly reducing equipment investment costs and operating costs.
  • the hydrogen and other phase media as the reaction raw materials enter the micro-interface generator 2 before entering the reactor body 1, and the mechanical microstructure and/or turbulent microstructure inside it
  • Microchannel action, field force action or mechanical energy action breaks the liquid and/or hydrogen during the hydrogenation reaction process into microbubbles and/or microdroplets with a diameter on the order of microns to form microinterfaces, micronanointerfaces or Ultra-micro interface, etc.; then fully mixed with other reaction phases to form multi-phase micro-mixed flow, multi-phase micro-nano flow, multi-phase emulsification flow, multi-phase micro-structure flow, gas-liquid-solid micro-mixed flow, gas-liquid-solid micro-nano flow, Gas-liquid-solid emulsified flow, gas-liquid-solid microstructure flow, microbubble, microbubble flow, microfoam, microfoam flow, microgas liquid flow, gas-liquid micro-nano emulsion flow, ultra micro flow, micro dispersion flow, two micro Micro Micro
  • the mass transfer area of the phase boundary further improves the mass transfer efficiency between hydrogen and each reaction phase during the hydrogenation reaction, and finally achieves the intensified heating within the range of 10%-80% of the pressure required by the existing intensified reaction system.
  • the purpose of the hydrogen reaction At the same time, it effectively solves the problems of high temperature, high pressure, high material consumption, high investment, high safety risk, etc. in the traditional hydrogenation process, thereby significantly reducing equipment investment costs and operating costs.
  • the reactor main body 1 serves as the main place where each reaction raw material reacts during the hydrogenation reaction, and the whole is a shell structure, which can specifically be: a tank reactor, a tubular reactor, a tower
  • Different reaction phases can be selected from any type of reactor such as emulsified bed reactor, suspended bed reactor, and fluidized bed reactor.
  • the specific type and structure of the reactor body 1 may be based on different application fields such as chemical industry, metallurgy, bioengineering, petrochemical industry, medicine, environment, and biochemistry, process parameters such as reaction temperature and reaction pressure, and reaction products. Quality requirements and other parameters are selected or designed, as long as it can ensure that the use requirements can be met to the greatest extent during the reaction process, that is, to maximize the reaction rate, improve the quality of the finished product, reduce cost input and ensure safe operation. It is understandable that the specific structure of the reactor main body 1 in different fields or different reaction processes inevitably has a certain degree of difference, for example, the positions and numbers of the inlet and outlet ports are not the same.
  • the micro-interface generator 2 is used as the core equipment for crushing gas and/or liquid in the hydrogenation reaction process. It is provided with a gas and/or liquid feed port on the reactor body 1, and the The gas and/or liquid phase in the hydrogenation reaction process converts the mechanical energy of the gas and/or liquid phase through the mechanical microstructure and/or turbulent microstructure through microchannel action, field force action or mechanical energy action, etc.
  • the surface energy of the gas phase and/or liquid phase which breaks the gas phase and/or liquid phase into micro-scale micro-bubbles and/or micro-droplets with a diameter of 1-1000 ⁇ m, and forms a micro-flow interface with other reaction phases System, thereby effectively increasing the mass transfer area of the phase boundary between the gas and/or liquid phase and the liquid and/or solid phase during the hydrogenation reaction process, greatly improving the mass transfer between the reaction phases Efficiency, finally achieves the purpose of strengthening the hydrogenation reaction under lower temperature and pressure conditions, and at the same time effectively solves the problems of high temperature, high pressure, high material consumption, high investment, and high safety risks in the traditional hydrogenation process. This significantly reduces equipment investment costs and operating costs.
  • the micro-interface generator 2 is connected in front of the feed port of the reactor main body 1, and its specific position and number can be based on the specific position of the gas and/or liquid phase feed port on the reactor main body 1. It can be set separately at the top, bottom or side of the reactor to form corresponding top-mounted, bottom-mounted and side-mounted micro-interface intensified hydrogenation reaction systems. It can also be installed at the top of the reactor at the same time. The bottom and sides are used to form a variety of opposing micro-interface strengthening hydrogenation reaction systems. At the same time, the micro-interface generator 2 is arranged inside and/or outside the reactor body 1.
  • the specific method for the micro-interface generator to break the gas phase and/or the liquid phase in the hydrogenation reaction can also be selected according to specific process requirements.
  • One of the microchannel action mode, field force action mode, and mechanical energy action mode can also be selected.
  • the micro-channel action mode is by constructing the micro-structure of the flow channel, so that the gas and/or liquid phase passing through the micro-channel is broken into micro bubbles and/or micro droplets, such as micropores Aeration method, micro-nanoporous membrane method (various metal membranes, inorganic membranes or organic membranes), micro-channel method or micro-fluidic method, etc.
  • the field force action method is the use of pressure field, high gravity field, ultrasonic field or The electromagnetic wave field and other external field forces input energy into the fluid in a non-contact manner, causing it to break into the microbubbles or microdroplets
  • the mechanical energy action method is to use the mechanical energy of the fluid to convert it into bubbles or droplets on the surface Yes
  • the hydrogen and other reaction media required for the reaction enter the reactor body 1 before entering the reactor body 1 through microchannels, field forces, or mechanical energy.
  • the liquid is broken into micron-level micro-bubbles and/or micro-droplets with a diameter of 1 ⁇ m ⁇ de ⁇ 1mm to form micro-interface, micro-nano interface or ultra-micro interface, etc., effectively increasing the hydrogenation reaction
  • the mass transfer area of the phase boundary between the gas and/or liquid phase and the liquid and/or solid phase in the process thereby improving the mass transfer efficiency between the reaction phases in the reaction process, and finally achieving the reaction in the existing enhanced reaction system
  • FIG. 1 it is a micro-interface strengthening hydrogenation reaction system of an embodiment of the present invention, which includes: a reactor main body 1 and a micro-interface generator 2; wherein the reactor main body 1 is a tank reactor for The reaction chamber for the hydrogenation reaction to ensure that the hydrogenation reaction can be fully carried out; the micro-interface generator 2 is connected to the gas-phase inlet and/or the liquid-phase inlet on the outer side of the tank reactor, and the set number is one, The hydrogen and liquid and/or solid-liquid mixture materials used in the hydrogenation reaction process pass the hydrogen and/or liquid phase reactants through the micro-interface generator before entering the reactor body.
  • the reactor main body 1 is a tank reactor for The reaction chamber for the hydrogenation reaction to ensure that the hydrogenation reaction can be fully carried out
  • the micro-interface generator 2 is connected to the gas-phase inlet and/or the liquid-phase inlet on the outer side of the tank reactor, and the set number is one,
  • the method is broken into micro-sized bubbles and/or micro-droplets with a diameter of 1 ⁇ m ⁇ de ⁇ 1mm, and forms a microfluidic interface system with other reaction phases to increase the gas and/or liquid phases during the hydrogenation reaction.
  • the mass transfer area of the phase boundary between the phase and the liquid phase and/or the solid phase improves the mass transfer efficiency between the reaction phases, and achieves the purpose of strengthening the hydrogenation reaction under preset temperature and pressure conditions.
  • the hydrogen and liquid and/or solid-liquid mixtures as raw materials for the reaction enter the micro-interface generator 2 before entering the tank reactor and are crushed by the micro-channel method and the impinging stream crushing method.
  • the reaction pressure in the tank reactor is 20%-50% of the internal pressure of the existing tank reactor, and the reaction temperature is 87%-90% of the existing reaction temperature, which greatly reduces the reaction
  • the energy consumption and production cost in the process reduce the investment intensity, prolong the equipment operation cycle, ensure the poor intrinsic safety in the reaction process, and effectively ensure the industrialized mass production of the reaction product.
  • the reaction described in this embodiment is a type of reaction in which a tank reactor is used for reaction enhancement.
  • the type of catalyst is not specifically limited. It can be an iron-based catalyst, a molybdenum-based catalyst, or a nickel-based catalyst.
  • FIG. 2 it is a tubular micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention, which includes: a reactor main body 1 and a micro-interface generator 2; wherein the reactor main body 1 is a tubular reactor for As a reaction chamber for the hydrogenation reaction, to ensure that the hydrogenation reaction can fully proceed; the micro-interface generator 2 is simultaneously arranged at the outer top of the tubular reactor before the gas phase inlet and/or the liquid phase inlet and the tube reactor Internally, used for the hydrogen and liquid and/or solid-liquid mixture materials in the hydrogenation reaction process to transfer the hydrogen and/or liquid phase reactants in the micro-interface generator before entering the reactor body 2.
  • the second step it is broken into micro-sized bubbles and/or micro-droplets with a diameter of 1 ⁇ m ⁇ de ⁇ 1mm by a preset method, and forms a microfluidic interface system with other reaction phases to increase the gas phase during the hydrogenation reaction. And/or the mass transfer area of the phase boundary between the liquid phase and the liquid phase and/or the solid phase to improve the mass transfer efficiency between the reaction phases, thereby achieving the enhancement of the hydrogenation reaction under the preset temperature and pressure conditions purpose.
  • the hydrogen and liquid and/or solid-liquid mixture materials used as reaction raw materials enter the micro-interface generator 2 before entering the tubular reactor and are broken by microporous aeration or impact
  • the method breaks into micro-bubbles and/or micro-droplets with a diameter of micrometers, and forms a microfluidic interface system with other reaction phases, and finally enters the tubular reactor to fully react under the action of the catalyst, and undergoes subsequent treatment To form different reaction products.
  • the system is in use: the reaction pressure in the tubular reactor is 30%-70% of the existing tubular reactor internal pressure, and the reaction temperature is 91%-94% of the existing reaction temperature, which greatly reduces the reaction temperature.
  • the reaction described in this embodiment is a type of reaction in which a tubular reactor is used for reaction enhancement. Therefore, the type of catalyst is not specifically limited, and it may be an iron-based catalyst, a molybdenum-based catalyst, or a nickel-based catalyst. One or several combinations of cobalt-based catalysts and tungsten-based catalysts, as long as it can ensure the smooth progress of the strengthening reaction.
  • FIG. 3 it is a tower type micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention, which includes: a reactor main body 1 and a micro-interface generator 2; wherein the reactor main body 1 is a tower reactor. Used as a reaction chamber for the hydrogenation reaction to ensure that the hydrogenation is fully carried out; the micro-interface generator 2 is connected to the gas phase inlet and/or the liquid phase inlet on the outside of the lower part of the tower reactor for The hydrogen and liquid and/or solid-liquid mixtures in the hydrogenation reaction process are crushed into the hydrogen and/or liquid phase reactants in the micro-interface generator 2 by a preset method before entering the reactor body.
  • the hydrogen and liquid and/or solid-liquid mixtures used as raw materials for the reaction enter the micro-interface generator 2 through the microporous aeration method and the microfluidic method.
  • One or more methods of Dao method, microfluidic method, pressure field, super-gravity field, ultrasonic field, electromagnetic wave field, impinging stream breaking method, cyclotron shear breaking method, spray method or gas-liquid mixed flow pump method Form micro-bubbles and/or micro-droplets with a diameter of micrometers, and form a microfluidic interface system with other reaction phases, and finally enter the tower reactor to fully react under the action of the catalyst, and undergo subsequent processing to form Different reaction products.
  • the reaction pressure in the tower reactor is 10%-55% of the internal pressure of the existing tower reactor, and the reaction temperature is 87-91% of the existing reaction temperature, which greatly reduces the reaction process.
  • the reaction described in this embodiment is a type of reaction in which a tower reactor is used for reaction enhancement. Therefore, the type of catalyst is not specifically limited, and it can be an iron-based catalyst, a molybdenum-based catalyst, or a nickel-based catalyst. One or several combinations of cobalt-based catalysts and tungsten-based catalysts, as long as it can ensure the smooth progress of the strengthening reaction.
  • FIG. 4 it is a fixed-bed micro-interface intensified hydrogenation reaction system of an embodiment of the present invention, which includes: a reactor body 1 and a micro-interface generator 2; wherein the reactor body 1 is a fixed-bed reactor. Used as a reaction chamber for the hydrogenation reaction to ensure that the hydrogenation reaction can fully proceed; the micro-interface generator 2 is respectively arranged in front of the gas phase inlet and/or the liquid phase inlet on the outer top of the fixed bed reactor.
  • the inside of the fixed-bed reactor is used for the hydrogen and liquid and/or solid-liquid mixture materials in the hydrogenation reaction process to transfer the hydrogen and/or liquid phase reactants in the reactor body before entering the reactor body
  • the micro-interface generator is broken into micro-bubbles and/or micro-droplets with a diameter of micrometers by a preset method, and forms a micro-fluid interface system with other reaction phases to increase the gas phase and/or micro-droplets during the hydrogenation reaction.
  • the mass transfer area of the phase boundary between the liquid phase and the liquid phase and/or the solid phase improves the mass transfer efficiency between the reaction phases, thereby achieving the purpose of strengthening the hydrogenation reaction under the preset temperature and pressure conditions.
  • the hydrogen and liquid and/or solid-liquid mixture materials used as reaction raw materials enter the micro-interface generator 2 before entering the fixed-bed reactor and are broken by micro-channel action or mechanical action.
  • the reaction pressure in the fixed bed reactor is 65%-80% of the existing fixed bed reactor internal pressure, and the reaction temperature is 90%-94% of the existing reaction temperature, which greatly reduces the reaction
  • the energy consumption and production cost in the process reduce the investment intensity, prolong the equipment operation cycle, ensure the poor intrinsic safety in the reaction process, and effectively ensure the industrialized mass production of the reaction product.
  • the reaction described in this embodiment is a type of reaction in which a fixed bed reactor is used for reaction enhancement. Therefore, the type of catalyst is not specifically limited. It can be an iron-based catalyst, a molybdenum-based catalyst, or a nickel-based catalyst. One or several combinations of cobalt-based catalysts and tungsten-based catalysts, as long as it can ensure the smooth progress of the strengthening reaction.
  • FIG. 5 it is an emulsion bed micro-interface strengthening hydrogenation reaction system of an embodiment of the present invention, which includes: a reactor main body 1 and a micro-interface generator 2; wherein the reactor main body 1 is an emulsion bed reactor.
  • the micro-interface generator 2 Used as the reaction chamber for the hydrogenation reaction to ensure that the hydrogenation reaction can fully proceed; the micro-interface generator 2 is connected to the gas phase inlet and/or liquid phase inlet on the side of the emulsified bed reactor, and the set number is Two, one of which is arranged outside the emulsified bed reactor, and the other is arranged inside the emulsified bed reactor, for the hydrogen and liquid and/or solid-liquid mixture in the hydrogenation process to enter Before the main body of the reactor, the hydrogen and/or liquid phase reactants are broken into micron-level micro-bubbles and/or micro-liquid with a diameter of 1 ⁇ m ⁇ de ⁇ 1mm in the micro-interface generator 2 by a preset method.
  • the mass transfer efficiency between the two to achieve the purpose of strengthening the hydrogenation reaction under the preset temperature and pressure conditions.
  • the hydrogen and liquid and/or solid-liquid mixtures used as raw materials for the reaction enter the micro-interface generator 2 to be broken by mechanical action and field force.
  • the reaction pressure in the emulsified bed reactor is 53%-76% of the internal pressure of the existing emulsified bed reactor, and the reaction temperature is 84%-89% of the existing reaction temperature, which greatly reduces the reaction temperature.
  • the energy consumption and production cost in the process reduce the investment intensity, prolong the equipment operation cycle, ensure the poor intrinsic safety in the reaction process, and effectively ensure the industrialized mass production of the reaction product.
  • the reaction described in this embodiment is a type of reaction in which an emulsion bed reactor is used for reaction enhancement. Therefore, the type of catalyst is not specifically limited. It can be an iron-based catalyst, a molybdenum-based catalyst, or a nickel-based catalyst. One or several combinations of cobalt-based catalysts and tungsten-based catalysts, as long as it can ensure the smooth progress of the strengthening reaction.
  • FIG. 6 it is a suspended bed micro-interface enhanced hydrogenation reaction system according to an embodiment of the present invention, which includes: a reactor body 1 and a micro-interface generator 2; wherein the reactor body 1 is a suspended bed reactor. Used as a reaction chamber for the hydrogenation reaction to ensure that the hydrogenation reaction can fully proceed; the micro-interface generator 2 is connected to the bottom end and the side gas inlet and/or liquid phase inlet of the suspended bed reactor. Before entering the main body of the reactor, the hydrogen and/or liquid and/or solid-liquid mixtures in the hydrogenation reaction process pass the hydrogen and/or liquid phase reactants through a preset in the micro-interface generator.
  • the method breaks into micro-sized bubbles and/or micro-droplets with a diameter of 1 ⁇ m ⁇ de ⁇ 1mm, and forms a microfluidic interface system with other reaction phases to increase the gas and/or liquid phase during the hydrogenation reaction
  • the mass transfer area of the phase boundary with the liquid phase and/or the solid phase improves the mass transfer efficiency between the reaction phases, thereby achieving the purpose of strengthening the hydrogenation reaction under the preset temperature and pressure conditions.
  • the hydrogen and liquid and/or solid-liquid mixtures as raw materials for the reaction enter the micro-interface generator 2 before entering the suspended bed reactor through micro-channel action and field force action.
  • the reaction pressure in the suspended bed reactor is 30%-48% of the existing traditional suspended bed (slurry bed) reactor internal pressure
  • the reaction temperature is 78%-84% of the existing reaction temperature
  • the reaction described in this embodiment is a type of reaction in which a suspended bed reactor is used for reaction enhancement. Therefore, the type of catalyst is not specifically limited. It can be an iron-based catalyst, a molybdenum-based catalyst, or a nickel-based catalyst. One or several combinations of cobalt-based catalysts and tungsten-based catalysts, as long as it can ensure the smooth progress of the strengthening reaction.
  • FIG. 7 it is a fluidized bed micro-interface strengthening hydrogenation reaction system of an embodiment of the present invention, which includes: a reactor body 1 and a micro-interface generator 2; wherein the reactor body 1 is a fluidized bed reactor, Used as a reaction chamber for the hydrogenation reaction to ensure that the hydrogenation reaction can fully proceed; the micro-interface generator 2 is connected to the gas phase inlet and/or the liquid phase inlet at the bottom and sides of the fluidized bed reactor. Before entering the reactor body, the hydrogen and liquid and/or solid-liquid mixtures in the hydrogenation reaction process pass the hydrogen and/or liquid reactants through the micro-interface generator 2.
  • the method is broken into micro-sized bubbles and/or micro-droplets with a diameter of 1 ⁇ m ⁇ de ⁇ 1mm, and forms a microfluidic interface system with other reaction phases to increase the gas and/or liquid phases during the hydrogenation reaction.
  • the mass transfer area of the phase boundary between the phase and the liquid phase and/or the solid phase improves the mass transfer efficiency between the reaction phases, thereby achieving the purpose of strengthening the hydrogenation reaction under the preset temperature and pressure conditions.
  • the hydrogen and liquid and/or solid-liquid mixtures as raw materials for the reaction enter the micro-interface generator 2 before entering the fluidized bed reactor through micro-channel action and field force action.
  • the reaction pressure in the fluidized bed reactor is 45%-78% of the internal pressure of the existing fluidized bed reactor, and the reaction temperature is 87%-93% of the existing reaction temperature, which greatly reduces the reaction
  • the energy consumption and production cost in the process reduce the investment intensity, prolong the equipment operation cycle, ensure the poor intrinsic safety in the reaction process, and effectively ensure the industrialized mass production of the reaction product.
  • the reaction described in this embodiment is a type of reaction in which a fluidized bed reactor is used for reaction enhancement. Therefore, the type of catalyst is not specifically limited. It can be an iron-based catalyst, a molybdenum-based catalyst, or a nickel-based catalyst. One or several combinations of cobalt-based catalysts and tungsten-based catalysts, as long as it can ensure the smooth progress of the strengthening reaction.
  • system of the present invention can also be used in various oxidation reactions, chlorination reactions, carbonylation reactions and combustible ice mining and other reaction processes to form micro-interface, micro-nano interface, ultra-micro interface, micro-bubble biochemical reactor or Microbubble bioreactors and other equipment, used micro mixing, micro fluidization, ultra micro fluidization, micro bubble fermentation, micro bubble bubbling, micro bubble mass transfer, micro bubble transfer, micro bubble reaction, micro bubble absorption, micro bubble Oxygen enhancement, microbubble contact and other processes or methods to make the material form multi-phase micro-mixed flow, multi-phase micro-nano flow, multi-phase emulsified flow, multi-phase micro-structured flow, gas-liquid-solid micro-mixed flow, gas-liquid-solid micro-nano flow, Gas-liquid-solid emulsified flow, gas-liquid-solid microstructure flow, microbubble, microbubble flow, microfoam, microfoam flow, microgas liquid flow, gas-liquid micro-
  • the micro-interface intensified hydrogenation reaction system provided by the present invention, by connecting the micro-interface generator to the main body of the reactor, the hydrogen and liquid and/or solid-liquid mixture materials in the hydrogenation reaction process enter the reaction Before the main body of the device, the hydrogen and/or liquid phase reactants are broken into micro bubbles and/or micro bubbles with a diameter of micrometers in the micro-interface generator through mechanical microstructures and/or turbulent microstructures in a preset mode of action.
  • the liquid droplets effectively increase the mass transfer area of the phase boundary between the hydrogen and the liquid and/or solid-liquid mixture during the reaction process, greatly improve the mass transfer efficiency between the reaction phases, and reach the preset pressure range
  • the purpose of internally strengthening the reaction while greatly reducing the energy consumption and production cost in the reaction process, reducing the investment intensity, extending the equipment operation cycle, ensuring the poor intrinsic safety of the reaction process, and effectively ensuring the industrialization of the reaction product Mass production.
  • different crushing methods can be selected according to the characteristics of different reaction phases and process requirements, such as microchannels, field forces or mechanical energy effects on the reaction medium.
  • the gas and/or liquid crushing effectively ensures the effectiveness of crushing the gas and/or liquid in the reaction medium before the reaction medium enters the main body of the reactor during the hydrogenation process, and ensures the gas, liquid and/or liquid phase and/or The mass transfer efficiency between the gas phase, the liquid phase and the solid phase further improves the reaction efficiency.

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Abstract

一种微界面强化加氢反应***，包括：反应器主体（1），用以作为加氢反应过程中的反应腔室；微界面发生器（2），与反应器主体（1）相连，用于在加氢反应过程中的氢气与液体和/或固液混合物料在进入反应器主体（1）之前将氢气和/或液相反应物在微界面发生器（2）中通过机械微结构和/或湍流微结构以预设作用方式破碎成直径为微米级别的微气泡和/或微液滴，以增大反应过程中氢气与液体和/或固液混合物料之间的相界传质面积，提高反应相之间的传质效率，在预设温度与压强条件下强化加氢反应。

Description

一种微界面强化加氢反应*** 技术领域
本发明属于反应强化技术领域，具体涉及一种微界面强化加氢反应***。
背景技术
能源、石化、精细化工等领域广泛存在气液、气液固等气液反应过程。如氧化、加氢、氯化等气液多相反应，其宏观反应速率一般受制于传质过程。气液反应的体积传质系数主要受到传质系数及气液相界面积的共同影响。已有研究表明，相界面积对体积传质系数的影响程度较大，且容易调控。因此，增大相界面积被视为提高气液宏观反应速率的有效途径。
鼓泡反应器和搅拌-鼓泡反应器是目前常用的气液反应器。如PX氧化制TA的塔式鼓泡反应器，气泡直径通常大于3mm，乃至厘米级，其传质界面面积有限。为提高宏观反应速率，必须通过增加鼓气量来促进液体湍流，使气泡破裂加剧以增加气泡数目，进而增大界面面积。而此举必然降低气体利用率，增大压缩机功率和尾气排放，导致能耗过渡和物料损失及环境污染。搅拌-鼓泡式气液反应器内多形成对气泡宏观运动有影响而对气泡破碎影响较小的大涡，气泡不能有效破碎，故直径偏大，传质面积受限，以致反应效率偏低。为强化气液传质，塔式鼓泡反应器一般在塔内增设塔板、静态混合器等内件以加强混合，而搅拌釜则需安装不同结构的搅拌桨或内筒等结构，以增加液层的含气量。这两种反应器，由于所得气泡直径通常为3-30mm，所提供的相界面积和传质系数(液侧、气侧、固液)有限，故反应性能较难获得突破性的提高。
发明内容
鉴于此，本发明提出了一种微界面强化加氢反应***，旨在解决现有的加氢反应强化***在进行反应强化的过程中通过高温高压的方式增大各反应相的相界面积，进而在提高传质速率的同时易造成能耗和生产成本高、投资强度大、设备操作周期短、故障多、本质安全性差等给工业化大规模生产带来挑战的问题。
本发明提出了一种微界面强化加氢反应***，包括：
反应器主体,其用以作为加氢反应过程中的反应腔室，以确保所述加氢反应能够充分进行；
微界面发生器(Micro Interfacial Generator，简称MIG)，其与所述反应器主体相连，用于在所述加氢反应过程中的氢气与液体和/或固液混合物料在进入所述反应器主体之前将所述氢气和/或液相反应物在所述微界面发生器中通过机械微结构和/或湍流微结构以预设作用方式破碎成直径为微米级别的微气泡和/或微液滴，以增大反应过程中所述氢气与所述液体和/或固液混合物料之间的相界传质面积，提高反应相之间的传质效率，在预设温度与压力条件下强化所述反应加氢反应速率。
进一步地，上述微界面强化加氢反应***中，所述预设作用方式选自微通道作用方式、场力作用方式以及机械能作用方式中的一种或几种；其中，
所述微通道作用方式通过构造流道的微结构，使通过微流道的气相和/或液相破碎成微气泡和/或微液滴；
所述场力作用方式是利用外场力作用以非接触的方式为流体输入能量，使其破碎成所述微气泡或微液滴；
所述机械能作用方式是利用流体的机械能，将其转换成气泡或液滴的表面能，使气泡或液滴破碎成所述微气泡或微液滴。
进一步地，上述微界面强化加氢反应***中，所述微通道作用方式选自微孔通气法、微纳孔膜法、微流道法以及微流控法中的一种或几种。
进一步地，上述微界面强化加氢反应***中，所述场力作用方式包括：压 力场作用、超重力场作用、超声波场作用或电磁波场作用。
进一步地，上述微界面强化加氢反应***中，所述机械能作用方式包括：撞击流破碎法、回旋剪切破碎法、喷雾法或气-液混流泵法。
进一步地，上述微界面强化加氢反应***中，所述反应器主体包括：釜式反应器、管式反应器、塔式反应器、固定床反应器或流化床反应器。
进一步地，上述微界面强化加氢反应***中，所述微界面发生器的连接在所述反应器主体的气相和/或液相进口端，其设置数量至少为一组。
进一步地，上述微界面强化加氢反应***中，所述预设压强范围为现有加氢强化反应***反应所需压力的10％-80％。
进一步地，上述微界面强化加氢反应***中，所述微米级别的范围为大于等于1μm、且小于1mm。
进一步地，上述微界面强化加氢反应***中，所述微界面强化加氢反应***可适用于化工、冶金、生物工程、石油化工、医药、环境治理、生化发酵、炼油、水产养殖、精细化工、生物发酵以及矿产开采领域的加氢反应。
与现有技术相比，本发明的有益效果在于，本发明提供的微界面强化加氢反应***，通过在反应器主体上连接微界面发生器，在所述加氢反应过程中的氢气与液体和/或固液混合物料在进入所述反应器主体之前将所述氢气和/或液相反应物在所述微界面发生器中通过机械微结构和/或湍流微结构以预设作用方式破碎成直径为微米级别的微气泡和/或微液滴，有效地增大了反应过程中氢气与液体和/或固液混合物料之间的相界传质面积，极大地提高反应相之间的传质效率，进而达到了在较低的预设压强范围内强化反应的目的，同时极大地减少了反应过程中的能耗和生产成本、降低了投资强度、延长了设备操作周期、确保了反应过程中的本质安全性差，有效地保证了反应成品的工业化大规模生产。
尤其是，本发明提供的微界面强化加氢反应***中，可以根据不同的反应相的自身特性与工艺需求选择不同的破碎方式，例如通过微通道、场力作用或 机械能作用对反应介质中的气体和/或液体进行破碎，有效地确保了在加氢过程中反应介质进入反应器主体之前对反应介质中气体和/或液体破碎的有效度，保证了反应过程中气相、液相和/或气相、液相以及固相之间的相界传质效率，进一步提升了反应效率。
附图说明
通过阅读下文优选实施方式的详细描述，各种其它的优点和益处对于本领域普通技术人员将变得清楚明了。附图仅用于示出优选实施方式的目的，而并不认为是对本发明的限制。而且在整个附图中，用相同的参考符号表示相同的部件。在附图中：
图1为本发明实施例的釜式微界面强化加氢反应***的结构示意图；
图2为本发明实施例的管式微界面强化加氢反应***的结构示意图；
图3为本发明实施例的塔式微界面强化加氢反应***的结构示意图；
图4为本发明实施例的固定床微界面强化加氢反应***的结构示意图；
图5为本发明实施例的乳化床微界面强化加氢反应***的结构示意图；
图6为本发明实施例的悬浮床微界面强化加氢反应***的结构示意图；
图7为本发明实施例的沸腾床微界面强化加氢反应***的结构示意图。
具体实施方式
下面将结合本发明实施例中的附图，对本发明实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例仅仅是本发明一部分实施例，而不是全部的实施例。基于本发明中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其它实施例，都属于本发明保护的范围。
参阅图1-7所示，为本发明实施例的微界面强化加氢反应***，其包括:反应器主体1和微界面发生器(MIG)2；其中，反应器主体1用以作为加氢反应过程中的反应腔室，以确保所述加氢反应能够充分进行；微界面发生器2 与所述反应器主体1相连，用于在所述加氢反应过程中的氢气与液体和/或固液混合物料在进入所述反应器主体之前将所述氢气和/或液相反应物在所述微界面发生器中通过机械微结构和/或湍流微结构以预设作用方式破碎成直径为微米级别的微气泡和/或微液滴，以在其它反应相中形成微界面、微纳界面、超微界面等，并与其它反应相共同形成如多相微混流、多相微纳流、多相乳化流、多相微结构流、气液固微混流、气液固微纳流、气液固乳化流、气液固微结构流、微气泡、微气泡流、微泡沫、微泡沫流、微气液流、气液微纳乳化流、超微流、微分散流、两相微混流、微湍流、微泡流、微鼓泡、微鼓泡流、微纳鼓泡以及微纳鼓泡流等由微米尺度颗粒形成的多相流体、或由微纳尺度颗粒形成的多相流体(简称微界面流体)，，进而有效地增大了加氢反应过程中所述气相和/或液相与液相和/或固相之间的相界传质面积，极大地提高了氢气与各反应相之间的传质效率，最终实现了在较低的预设温度与压强条件下强化所述加氢反应的目的，同时有效地解决传统加氢反应过程中高温、高压、高物耗、高投资、高安全风险等问题，由此显著地降低设备的投资成本和运行费用。
本实施例中，作为反应原料的氢气与其它各相介质在进入所述反应器主体1之前，先进入所述微界面发生器2中，通过其内部的机械微结构和/或湍流微结构以微通道作用、场力作用或机械能作用等方式将所述加氢反应过程中的液体和/或氢气破碎成直径在微米级别的微气泡和/或微液滴，形成微界面、微纳界面或超微界面等；然后与其它反应相充分混合，形成如多相微混流、多相微纳流、多相乳化流、多相微结构流、气液固微混流、气液固微纳流、气液固乳化流、气液固微结构流、微气泡、微气泡流、微泡沫、微泡沫流、微气液流、气液微纳乳化流、超微流、微分散流、两项微混流、微湍流、微泡流、微鼓泡、微鼓泡流、微纳鼓泡以及微纳鼓泡流等微界面流体反应体系；最后通过所述反应器主体1的进料口进入所述反应器主体1内部在催化剂的作用下充分反应，并经后续处理以形成不同的反应产物，进而有效地增大了反应过程中氢气和/或液相与液相和/或固相之间的相界传质面积，进而提高了加氢反应过程中氢 气与各反应相之间的传质效率，最终达到了在现有强化反应***反应所需压力的10％-80％压强范围内强化加氢反应的目的；同时有效地解决传统加氢反应过程中高温、高压、高物耗、高投资、高安全风险等问题，由此显著地降低设备的投资成本和运行费用。
具体而言，所述反应器主体1作为加氢反应过程中各反应原料进行反应的主要发生场所，其整体为一壳体构造，具体可以为：釜式反应器、管式反应器、塔式反应器、固定床反应器以及流化床反应器，只要能够作为加氢反应的反应腔室，确保所述加氢反应能够充分进行反应即可，其中流化床反应器又可以根据反应原料中反应相的不同选取乳化床反应器、悬浮床反应器以及沸腾床反应器等任意形式的反应器。
本实施例中，所述反应器主体1的具体类型和构造可以根据化工、冶金、生物工程、石油化工、医药、环境以及生化等不同使用领域、反应温度和反应压强等工艺参数以及反应生成品质量需求等参数进行选择或设计，只要能够确保在反应过程能够最大限度满足使用需求，即最大限度的提升反应速率、提高成品质量、降低成本投入以及保证安全操作即可。可以理解的是，不同领域或不同反应工艺中反应器主体1的具体结构必然存在一定程度的差异，例如进出料口的设置位置和数量等不尽相同。
具体而言，所述微界面发生器2作为加氢反应过程中破碎气体和/或液体的核心设备，其设置所述反应器主体1上的气相和/或液相进料口，将所述加氢反应过程中的气相和/或液相通过机械微结构和/或湍流微结构以微通道作用、场力作用或机械能作用等方式将加氢反应过程中气相和/或液相的机械能转换成气相和/或液相的表面能，进而使气相和/或液相破碎成直径为1-1000μm之间的微米级别的微气泡和/或微液滴，并与其它反应相形成微流界面体系，进而有效地增大了加氢反应过程中所述气相和/或液相与液相和/或固相之间的相界传质面积，极大地提高了各反应相之间的传质效率，最终实现了在较低的温度与压强条件下强化所述加氢反应的目的，同时有效地解决传统加 氢反应过程中高温、高压、高物耗、高投资、高安全风险等问题，由此显著地降低设备的投资成本和运行费用。
本实施例中，所述微界面发生器2连接在所述反应器主体1的进料口之前，其具***置和数量可以根据反应器主体1上气相和/或液相进料口的具***置和数量而确定，例如可单独地设置在反应器的顶部、底部或侧部，以形成对应的上置式、下置式以及侧置式微界面强化加氢反应***，也可以同时设置在反应器顶部、底部以及侧部，以形成多种对冲式微界面强化加氢反应***。同时，微界面发生器2设置在反应器主体1的内部和/或外部。尤其是，所述微界面发生器破碎所述加氢反应中气相和/或液相的具体方式也可以根据具体的工艺需求进行选择微通道作用方式、场力作用方式以及机械能作用方式中的一种或几种进行组合；其中，所述微通道作用方式是通过构造流道的微结构，使通过微流道的气相和/或液相破碎成微气泡和/或微液滴，例如微孔通气法、微纳孔膜法(各种金属膜、无机膜或有机膜)、微流道法或微流控法等；所述场力作用方式是利用压力场、超重力场、超声波场或电磁波场等外场力作用以非接触的方式为流体输入能量，使其破碎成所述微气泡或微液滴；所述机械能作用方式是利用流体的机械能，将其转换成气泡或液滴的表面能，使气泡或液滴破碎成所述微气泡或微液滴，其包括：撞击流破碎法、回旋剪切破碎法、喷雾法以及气-液混流泵法等。使用的过程中，反应所需的氢气与其它反应介质在进入所述反应器主体1之前先进入其内部通过微通道、场力作用或机械能作用等方式将所述加氢反应过程中的气体和/或液体破碎成微米级别的直径为1μm≤de<1mm的微米级别的微气泡和/或微液滴，以形成微界面、微纳界面或超微界面等，有效地增大了加氢反应过程中气相和/或液相与液相和/或固相之间的相界传质面积，进而提高反应过程中各反应相之间的传质效率，最终达到了在现有强化反应***反应所需压力的10％-80％压强范围内强化加氢反应的目的；同时有效地解决传统加氢反应过程中高温、高压、高物耗、高投资、高安全风险等问题，由此显著地降低设备的投资成本和运行费用。
继续参阅图1所示，为本发明实施例的微界面强化加氢反应***，其包括：反应器主体1和微界面发生器2；其中，反应器主体1为釜式反应器，用以作为加氢反应的反应腔室，以确保所述加氢反应能够充分进行；微界面发生器2连接在所述釜式反应器外侧部的气相进口和/或液相进口，其设置数量为一个，用于在所述加氢反应过程中的氢气与液体和/或固液混合物料在进入所述反应器主体之前将所述氢气和/或液相反应物在所述微界面发生器中通过预设方法破碎成直径为1μm≤de<1mm的微米级别的微气泡和/或微液滴，并与其它反应相形成微流界面体系，以增大加氢反应过程中所述气相和/或液相与液相和/或固相之间的相界传质面积，提高各反应相之间的传质效率，实现了在预设温度与压强条件下强化所述加氢反应的目的。本实施例中，作为反应原料的氢气与液体和/或固液混合物料在进入所述釜式反应器之前，先进入所述微界面发生器2中通过微流道法和撞击流破碎法破碎成直径为微米级别的微气泡和/或微液滴，并与其它反应相形成微流界面体系，最后进入所述釜式反应器内部在催化剂的作用下进行充分反应，并经后续处理以形成不同的反应产物。本***在使用过程中：釜式反应器内反应压力为现有釜式反应器内部压力的20％-50％，反应温度为现有反应温度的87％-90％，进而极大地减少了反应过程中的能耗和生产成本、降低了投资强度、延长了设备操作周期、确保了反应过程中的本质安全性差，有效地保证了反应成品的工业化大规模生产。可以理解的是，本实施例中的所述的反应为采用釜式反应器进行反应强化的一类反应，因此不具体限定催化剂的种类，其可以为铁系催化剂、钼系催化剂、镍系催化剂、钴系催化剂以及钨系催化剂中的一种或几种组合，只要能够确保强化反应顺利进行即可。。
继续参阅图2所示，为本发明实施例的管式微界面强化加氢反应***，其包括：反应器主体1和微界面发生器2；其中，反应器主体1为管式反应器，用以作为加氢反应的反应腔室，以确保加氢反应能够充分进行；微界面发生器2同时设置在所述管式反应器的外部顶端气相进口和/或液相进口之前和管式 反应器的内部，，用于在所述加氢反应过程中的氢气与液体和/或固液混合物料在进入所述反应器主体之前将所述氢气和/或液相反应物在所述微界面发生器2中通过预设方法破碎成直径为1μm≤de<1mm的微米级别的微气泡和/或微液滴，并与其它反应相形成微流界面体系，以增大加氢反应过程中所述气相和/或液相与液相和/或固相之间的相界传质面积，提高各反应相之间的传质效率，进而实现在预设温度与压强条件下强化所述加氢反应的目的。具体的，本实施例中，作为反应原料的氢气与液体和/或固液混合物料在进入所述管式反应器之前，先进入所述微界面发生器2中通过微孔通气法或撞击破碎法破碎成直径为微米级别的微气泡和/或微液滴，并与其它反应相形成微流界面体系，最后进入所述管式反应器内部在催化剂的作用下进行充分反应，并经后续处理以形成不同的反应产物。本***在使用过程中：管式反应器内反应压力为现有管式反应器内部压力的30％-70％，反应温度为现有反应温度的91％-94％，进而极大地减少了反应过程中的能耗和生产成本、降低了投资强度、延长了设备操作周期、确保了反应过程中的本质安全性差，有效地保证了反应成品的工业化大规模生产。可以理解的是，本实施例中的所述的反应为采用管式反应器进行反应强化的一类反应，因此不具体限定催化剂的种类，其可以为铁系催化剂、钼系催化剂、镍系催化剂、钴系催化剂以及钨系催化剂中的一种或几种组合，只要能够确保强化反应顺利进行即可。
继续参阅图3所示，为本发明实施例的塔式微界面强化加氢反应***，其包括：反应器主体1和微界面发生器2；其中，反应器主体1为塔式反应器，用以作为加氢反应的反应腔室，以确保所述加氢充分进行；微界面发生器2连接在所述塔式反应器下部外侧的气相进口和/或液相进口之前，用于在所述加氢反应过程中的氢气与液体和/或固液混合物料在进入所述反应器主体之前将所述氢气和/或液相反应物在所述微界面发生器2中通过预设方法破碎成直径为1μm≤de<1mm的微米级别的微气泡和/或微液滴，并与其它反应相形成微流界面体系，以增大加氢反应过程中所述气相和/或液相与液相和/或固相之间 的相界传质面积，提高各反应相之间的传质效率，进而实现在预设温度与压强条件下强化所述加氢反应的目的。具体的，本实施例中，作为反应原料的氢气与液体和/或固液混合物料在进入所述塔式反应器之前，先进入所述微界面发生器2中通过微孔通气法、微流道法、微流控法、压力场、超重力场、超声波场、电磁波场、撞击流破碎法、回旋剪切破碎法、喷雾法或气-液混流泵法中的一种或几种方式破碎成直径为微米级别的微气泡和/或微液滴，并与其它反应相形成微流界面体系，最后进入所述塔式反应器内部在催化剂的作用下进行充分反应，并经后续处理以形成不同的反应产物。本***在使用过程中：塔式反应器内反应压力为现有塔式反应器内部压力的10％-55％，反应温度为现有反应温度的87-91％，进而极大地减少了反应过程中的能耗和生产成本、降低了投资强度、延长了设备操作周期、确保了反应过程中的本质安全性差，有效地保证了反应成品的工业化大规模生产。可以理解的是，本实施例中的所述的反应为采用塔式反应器进行反应强化的一类反应，因此不具体限定催化剂的种类，其可以为铁系催化剂、钼系催化剂、镍系催化剂、钴系催化剂以及钨系催化剂中的一种或几种组合，只要能够确保强化反应顺利进行即可。
继续参阅图4所示，为本发明实施例的固定床微界面强化加氢反应***，其包括：反应器主体1和微界面发生器2；其中，反应器主体1为固定床反应器，用以作加氢反应的反应腔室，以确保所述加氢反应能够充分进行；微界面发生器2分别设置在所述固定床反应器的外部顶端的气相进口和/或液相进口之前和所述固定床反应器内部，用于在所述加氢反应过程中的氢气与液体和/或固液混合物料在进入所述反应器主体之前将所述氢气和/或液相反应物在所述微界面发生器中通过预设方法破碎成直径为微米级别的微气泡和/或微液滴，并与其它反应相形成微流界面体系，以增大加氢反应过程中所述气相和/或液相与液相和/或固相之间的相界传质面积，提高各反应相之间的传质效率，进而实现在预设温度与压强条件下强化所述加氢反应的目的。具体的，本实施例中，作为反应原料的氢气与液体和/或固液混合物料在进入所述固定床反应 器之前，先进入所述微界面发生器2中通过微通道作用或机械作用破碎成直径为1μm≤de<1mm的微米级别的微气泡和/或微液滴，并与其它反应相形成微流界面体系，最后进入所述固定床反应器内部在催化剂的作用下进行充分反应，并经后续处理以形成不同的反应产物。本***在使用过程中：固定床反应器内反应压力为现有固定床反应器内部压力的65％-80％，反应温度为现有反应温度的90％-94％，进而极大地减少了反应过程中的能耗和生产成本、降低了投资强度、延长了设备操作周期、确保了反应过程中的本质安全性差，有效地保证了反应成品的工业化大规模生产。可以理解的是，本实施例中的所述的反应为采用固定床反应器进行反应强化的一类反应，因此不具体限定催化剂的种类，其可以为铁系催化剂、钼系催化剂、镍系催化剂、钴系催化剂以及钨系催化剂中的一种或几种组合，只要能够确保强化反应顺利进行即可。
继续参阅图5所示，为本发明实施例的乳化床微界面强化加氢反应***，其包括：反应器主体1和微界面发生器2；其中，反应器主体1为乳化床反应器，用以作为加氢反应的反应腔室，以确保所述加氢反应能够充分进行；微界面发生器2连接在所述乳化床反应器侧部的气相进口和/或液相进口，且设置数量为两个，其中一个设置在所述乳化床反应器外部、另一设置在所述乳化床反应器内部，用于在所述加氢反应过程中的氢气与液体和/或固液混合物料在进入所述反应器主体之前将所述氢气和/或液相反应物在所述微界面发生器2中通过预设方法破碎成直径为1μm≤de<1mm的微米级别的微气泡和/或微液滴，并与其它反应相形成微流界面体系，以增大加氢反应过程中所述气相和/或液相与液相和/或固相之间的相界传质面积，提高各反应相之间的传质效率，进而实现在预设温度与压强条件下强化所述加氢反应的目的。具体的，本实施例中，作为反应原料的氢气与液体和/或固液混合物料在进入所述乳化床反应器之前，先进入所述微界面发生器2中通过机械作用和场力作用破碎成直径为微米级别的微气泡和/或微液滴，并与其它反应相形成微流界面体系，最后进入所述乳化床反应器内部在催化剂的作用下进行充分反应，并经后续处理以形 成不同的反应产物。本***在使用过程中：乳化床反应器内反应压力为现有乳化床反应器内部压力的53％-76％，反应温度为现有反应温度的84％-89％，进而极大地减少了反应过程中的能耗和生产成本、降低了投资强度、延长了设备操作周期、确保了反应过程中的本质安全性差，有效地保证了反应成品的工业化大规模生产。可以理解的是，本实施例中的所述的反应为采用乳化床反应器进行反应强化的一类反应，因此不具体限定催化剂的种类，其可以为铁系催化剂、钼系催化剂、镍系催化剂、钴系催化剂以及钨系催化剂中的一种或几种组合，只要能够确保强化反应顺利进行即可。
继续参阅图6所示，为本发明实施例的悬浮床微界面强化加氢反应***，其包括：反应器主体1和微界面发生器2；其中，反应器主体1为悬浮床反应器，用以作为加氢反应的反应腔室，以确保所述加氢反应能够充分进行；微界面发生器2连接在所述悬浮床反应器的底端和侧部气相进口和/或液相进口，用于在所述加氢反应过程中的氢气与液体和/或固液混合物料在进入所述反应器主体之前将所述氢气和/或液相反应物在所述微界面发生器中通过预设方法破碎成直径为1μm≤de<1mm的微米级别的微气泡和/或微液滴，并与其它反应相形成微流界面体系，以增大加氢反应过程中所述气相和/或液相与液相和/或固相之间的相界传质面积，提高各反应相之间的传质效率，进而实现在预设温度与压强条件下强化所述加氢反应的目的。具体的，本实施例中，作为反应原料的氢气与液体和/或固液混合物料在进入所述悬浮床反应器之前，先进入所述微界面发生器2中通过微通道作用和场力作用破碎成直径为微米级别的微气泡和/或微液滴，并与其它反应相形成微流界面体系，最后进入所述悬浮床反应器内部在催化剂的作用下进行充分反应，并经后续处理以形成不同的反应产物。本***在使用过程中：悬浮床反应器内反应压力为现有传统的悬浮床(浆态床)反应器内部压力的30％-48％，反应温度为现有反应温度的78％-84％，进而极大地减少了反应过程中的能耗和生产成本、降低了投资强度、延长了设备操作周期、确保了反应过程中的本质安全性差，有效地保证了反应成品的工业 化大规模生产。可以理解的是，本实施例中的所述的反应为采用悬浮床反应器进行反应强化的一类反应，因此不具体限定催化剂的种类，其可以为铁系催化剂、钼系催化剂、镍系催化剂、钴系催化剂以及钨系催化剂中的一种或几种组合，只要能够确保强化反应顺利进行即可。
继续参阅图7所示，为本发明实施例的沸腾床微界面强化加氢反应***，其包括：反应器主体1和微界面发生器2；其中，反应器主体1为沸腾床反应器，用以作为加氢反应的反应腔室，以确保所述加氢反应能够充分进行；微界面发生器2连接在所述沸腾床反应器底端和侧部的气相进口和/或液相进口，用于在所述加氢反应过程中的氢气与液体和/或固液混合物料在进入所述反应器主体之前将所述氢气和/或液相反应物在所述微界面发生器2中通过预设方法破碎成直径为1μm≤de<1mm的微米级别的微气泡和/或微液滴，并与其它反应相形成微流界面体系，以增大加氢反应过程中所述气相和/或液相与液相和/或固相之间的相界传质面积，提高各反应相之间的传质效率，进而实现在预设温度与压强条件下强化所述加氢反应的目的。具体的，本实施例中，作为反应原料的氢气与液体和/或固液混合物料在进入所述沸腾床反应器之前，先进入所述微界面发生器2中通过微通道作用、场力作用或机械作用下破碎成直径为微米级别的微气泡和/或微液滴，并与其它反应相形成微流界面体系，最后进入所述沸腾床反应器内部在催化剂的作用下进行充分反应，并经后续处理以形成不同的反应产物。本***在使用过程中：沸腾床反应器内反应压力为现有沸腾床反应器内部压力的45％-78％，反应温度为现有反应温度的87％-93％，进而极大地减少了反应过程中的能耗和生产成本、降低了投资强度、延长了设备操作周期、确保了反应过程中的本质安全性差，有效地保证了反应成品的工业化大规模生产。可以理解的是，本实施例中的所述的反应为采用沸腾床反应器进行反应强化的一类反应，因此不具体限定催化剂的种类，其可以为铁系催化剂、钼系催化剂、镍系催化剂、钴系催化剂以及钨系催化剂中的一种或几种组合，只要能够确保强化反应顺利进行即可。
此外，本发明所述***还可用于各类氧化反应、氯化反应、羰基化反应以及可燃冰开采等反应过程中，进而形成微界面、微纳界面、超微界面、微泡生化反应器或微泡生物反应器等设备，用过微混合、微流化、超微流化、微泡发酵、微泡鼓泡、微泡传质、微泡传递、微泡反应、微泡吸收、微泡增氧、微泡接触等工艺或方法，以使物料形成多相微混流、多相微纳流、多相乳化流、多相微结构流、气液固微混流、气液固微纳流、气液固乳化流、气液固微结构流、微气泡、微气泡流、微泡沫、微泡沫流、微气液流、气液微纳乳化流、超微流、微分散流、两项微混流、微湍流、微泡流、微鼓泡、微鼓泡流、微纳鼓泡以及微纳鼓泡流等微流体，从而提高相间的传质面积，以提高相间的反应效率。
显然，本发明提供的微界面强化加氢反应***，通过在反应器主体上连接微界面发生器，在所述加氢反应过程中的氢气与液体和/或固液混合物料在进入所述反应器主体之前将所述氢气和/或液相反应物在所述微界面发生器中通过机械微结构和/或湍流微结构以预设作用方式破碎成直径为微米级别的微气泡和/或微液滴，有效地增大了反应过程中氢气与液体和/或固液混合物料之间的相界传质面积，极大地提高反应相之间的传质效率，进而达到了在预设压强范围内强化反应的目的，同时极大地减少了反应过程中的能耗和生产成本、降低了投资强度、延长了设备操作周期、确保了反应过程中的本质安全性差，有效地保证了反应成品的工业化大规模生产。
尤其是，本发明提供的微界面强化加氢反应***中，可以根据不同的反应相的自身特性与工艺需求选择不同的破碎方式，例如通过微通道、场力作用或机械能作用对反应介质中的气体和/或液体进行破碎，有效地确保了在加氢过程中反应介质进入反应器主体之前对反应介质中气体和/或液体破碎的有效度，保证了反应过程中气相、液相和/或气相、液相以及固相之间的相界传质效率，进一步提升了反应效率。
显然，本领域的技术人员可以对本发明进行各种改动和变型而不脱离本发明的精神和范围。这样，倘若本发明的这些修改和变型属于本发明权利要求及 其等同技术的范围之内，则本发明也意图包含这些改动和变型在内。

Claims (10)

  1. 一种微界面强化加氢反应***，其特征在于，包括：
    反应器主体,其用以作为加氢反应过程中的反应腔室，以确保所述加氢反应能够充分进行；
    微界面发生器，其与所述反应器主体相连，用于在所述加氢反应过程中的氢气与液体和/或固液混合物料在进入所述反应器主体之前将所述氢气和/或液相反应物在所述微界面发生器中通过机械微结构和/或湍流微结构以预设作用方式破碎成直径为微米级别的微气泡和/或微液滴，以增大反应过程中所述氢气与所述液体和/或固液混合物料之间的相界传质面积，提高反应相之间的传质效率，在预设温度与压力条件下强化所述加氢反应速率。
  2. 根据权利要求1所述的微界面强化加氢反应***，其特征在于，所述预设作用方式选自微通道作用方式、场力作用方式以及机械能作用方式中的一种或几种；其中，
    所述微通道作用方式通过构造流道的微结构，使通过微流道的气相和/或液相破碎成微气泡和/或微液滴；
    所述场力作用方式是利用外场力作用以非接触的方式为流体输入能量，使其破碎成所述微气泡或微液滴；
    所述机械能作用方式是利用流体的机械能，将其转换成气泡或液滴的表面能，使气泡或液滴破碎成所述微气泡或微液滴。
  3. 根据权利要求2所述的微界面强化加氢反应***，其特征在于，所述微通道作用方式选自微孔通气法、微纳孔膜法、微流道法以及微流控法中的一种或几种。
  4. 根据权利要求2所述的微界面强化加氢反应***，其特征在于，所述场力作用方式包括：压力场作用、超重力场作用、超声波场作用或电磁波场作用。
  5. 根据权利要求2所述的微界面强化加氢反应***，其特征在于，所述 机械能作用方式包括：撞击流破碎法、回旋剪切破碎法、喷雾法或气-液混流泵法。
  6. 根据权利要求1-5任一所述的微界面强化加氢反应***，其特征在于，所述反应器主体包括：釜式反应器、管式反应器、塔式反应器、固定床反应器或流化床反应器。
  7. 根据权利要求6所述的微界面强化加氢反应***，其特征在于，所述微界面发生器的连接在所述反应器主体的气相和/或液相进口端，其设置数量至少为一组。
  8. 根据权利要求1所述的微界面强化加氢反应***，其特征在于，所述预设压强范围为现有强化反应***反应所需压力的10％-80％。
  9. 根据权利要求8所述的微界面强化加氢反应***，其特征在于，所述微米级别的范围为大于等于1μm、且小于1mm。
  10. 根据权利要求1-5或7-9任一所述的微界面强化加氢反应***，其特征在于，所述微界面强化加氢反应***可适用于化工、冶金、生物工程、石油化工、医药、环境治理、生化发酵、炼油、水产养殖、精细化工、生物发酵以及矿产开采领域的加氢反应。
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