WO2020186633A1 - Système de réaction amélioré par micro-interface - Google Patents

Système de réaction amélioré par micro-interface Download PDF

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WO2020186633A1
WO2020186633A1 PCT/CN2019/090253 CN2019090253W WO2020186633A1 WO 2020186633 A1 WO2020186633 A1 WO 2020186633A1 CN 2019090253 W CN2019090253 W CN 2019090253W WO 2020186633 A1 WO2020186633 A1 WO 2020186633A1
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micro
liquid
reaction
gas
phase
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PCT/CN2019/090253
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Chinese (zh)
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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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    • 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
    • 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
    • B01J19/0053—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
    • 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
    • B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
    • B01J3/02—Feed or outlet devices therefor
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • 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

Definitions

  • the invention belongs to the technical field of reaction strengthening, and specifically relates to a micro-interface strengthening reaction system.
  • the interface refers to the area between the material phase and the phase. It exists between the two phases and has a thickness of about several molecular layers to dozens of molecular layers. It is different from the concept of "face” in geometry. There are faces here. The thickness is the boundary area between the concrete phases.
  • the interface phenomenon occurs with mass transfer, and it has a significant impact on the mass transfer process. Extraction, distillation, absorption, gas-liquid reaction, liquid-liquid reaction, gas-liquid-solid three-phase reaction, etc. are all typical interface mass transfer processes. Although the existing multi-phase reaction system is highly adaptable to raw materials and simple to operate, the gas and/or liquid in the reaction medium has a large scale and the phase boundary area of the gas and/or liquid phase is relatively small.
  • the mass transfer area and mass transfer rate are severely restricted, which in turn affects the overall efficiency of the reaction.
  • the fundamental reason is that the bubble size in the reactor is relatively large (generally 3-30mm), so the mass transfer area of the gas-liquid phase boundary is small (generally 50-200m2/m3), which limits the mass transfer efficiency. Therefore, high temperature (above 470°C) and high pressure (above 30MPa) operations have to be used in engineering to increase the mass transfer rate by increasing the solubility of the gas and/or liquid phase, thereby strengthening the reaction process.
  • high temperature and high pressure produce a series of side effects: high energy consumption and production cost, high investment intensity, short equipment operation cycle, many failures, poor intrinsic safety, etc., which bring challenges to industrialized mass production.
  • the present invention proposes a micro-interface strengthening reaction system, which aims to solve the problem that the existing reaction strengthening system increases the phase boundary area of each reaction phase by means of high temperature and high pressure in the process of reaction strengthening, thereby increasing the transmission rate.
  • the existing reaction strengthening system increases the phase boundary area of each reaction phase by means of high temperature and high pressure in the process of reaction strengthening, thereby increasing the transmission 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 industrialized large-scale production.
  • the present invention proposes a micro-interface strengthening reaction system, including:
  • the main body of the reactor is used as a reaction chamber for the reaction of gas-liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid and liquid-liquid-solid multiphase reaction medium to ensure The multiphase reaction medium can fully react;
  • Micro Interfacial Generator (MIG for short), which is connected to the reactor main body and is used to remove the gas phase and/or the gas phase in the multiphase reaction medium before the multiphase reaction medium enters the reactor main body.
  • the liquid phase is broken into micro-bubbles and/or micro-droplets with a diameter of micrometers in the micro-interface generator through mechanical micro-structures and/or turbulent micro-structures in a predetermined action mode to increase
  • the mass transfer area of the phase boundary between the gas and/or liquid phase and the liquid and/or solid phase improves the mass transfer efficiency between the reaction phases and strengthens the multiplicity within the preset temperature and/or preset pressure range. Instead.
  • 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, 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 inlet end of the reactor body, and the number of the micro-interface generator is at least one set.
  • the preset pressure range is 50%-80% of the pressure required by the existing intensified reaction system.
  • the micron-level range is greater than or equal to 1 ⁇ m and less than 1 mm.
  • the micro-interface strengthening reaction system may be suitable for chemical industry, metallurgy, bioengineering, petrochemical industry, medicine, environmental treatment, biochemical fermentation, oil refining, aquaculture, fine chemical industry, biological fermentation and The field of mineral mining.
  • the beneficial effect of the present invention is that the micro-interface strengthening reaction system provided by the present invention connects the micro-interface generator to the main body of the reactor to react the multi-phase reaction before the multi-phase reaction medium enters the main body of the reactor.
  • the gas and/or liquid phase in the medium is broken into micro-bubbles and/or micro-droplets with a diameter of micrometers in the micro-interface generator through micro-channels, field forces or mechanical energy, effectively increasing the gas phase in the reaction process And/or the mass transfer area of the phase boundary between the liquid phase and the liquid and/or solid phase, which greatly enhances the mass transfer efficiency of each reaction phase during the reaction process, thereby achieving the enhancement of the reaction within the preset pressure range
  • the purpose is to greatly reduce the energy consumption and production cost in the reaction process, reduce the investment intensity, extend the equipment operation cycle, ensure the poor intrinsic safety in the reaction process, and effectively ensure the industrialized mass production of the reaction product.
  • different crushing methods can be selected according to the characteristics of different reaction phases and process requirements, for example, through microchannels, field forces or mechanical energy, the gas phase in the reaction medium And/or the liquid phase is broken, which effectively ensures the effectiveness of the gas and/or liquid phase in the reaction medium before the multiphase reaction medium enters the main body of the reactor, and ensures that the gas and/or liquid phase and liquid phase are broken during the reaction process.
  • the mass transfer efficiency of the phase boundary between the phase and/or solid phase further improves the reaction efficiency.
  • FIG. 1 is a schematic structural diagram of a kettle-type micro-interface strengthening reaction system according to an embodiment of the present invention
  • FIG. 2 is a schematic structural diagram of a tubular micro-interface strengthening reaction system according to an embodiment of the present invention
  • FIG. 3 is a schematic structural diagram of a tower-type micro-interface strengthening reaction system according to an embodiment of the present invention.
  • FIG. 4 is a schematic structural diagram of a fixed bed micro-interface strengthening reaction system according to an embodiment of the present invention.
  • FIG. 5 is a schematic structural diagram of an emulsion bed micro-interface strengthening reaction system according to an embodiment of the present invention.
  • FIG. 6 is a schematic structural diagram of a suspension bed micro-interface strengthening reaction system according to an embodiment of the present invention.
  • Fig. 7 is a schematic structural diagram of a fluidized bed micro-interface strengthening reaction system according to an embodiment of the present invention.
  • a micro-interface strengthening reaction system which includes: a reactor body 1 and a micro-interface generator (MIG) 2; wherein the reactor body 1 is used as a gas-liquid, Liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid, and liquid-liquid-solid multi-phase reaction media are reacted in a reaction chamber to ensure that the multi-phase reaction medium can fully react; micro-interface
  • the generator 2 is connected to the reactor main body 1, and is used to generate the gas phase and/or liquid phase in the multiphase reaction medium at the micro interface before the multiphase reaction medium enters the reactor main body 1.
  • the mechanical microstructure and/or the turbulent microstructure are broken into microbubbles and/or microdroplets with a diameter of micrometers in a predetermined action mode to form microinterfaces, micronanointerfaces, and ultramicro Interface, etc., and together with other reaction phases to form such as 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 emulsification Flow, gas-liquid-solid microstructure flow, microbubble, microbubble flow, microfoam, microfoam flow, micro-gas-liquid flow, gas-liquid micro-nano emulsified flow, ultra-micro flow, micro-dispersion flow, two micro-mixed flow, micro-turbulent flow , Microbubble flow, microbubble, microbubble flow, micro-nano bubble and micro-n
  • the gas-liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid, liquid-liquid-solid and other multiphase media as reaction raw materials enter the reactor body 1 Before, first enter the micro-interface generator 2 and combine the liquid in the multiphase reaction medium with the micro-channel action, field force action or mechanical energy action through its internal mechanical microstructure and/or turbulent microstructure.
  • the gas is broken into microbubbles and/or microdroplets with a diameter of 1 ⁇ m ⁇ de ⁇ 1mm, forming microinterfaces, micronanointerfaces or ultramicrointerfaces, etc.; then it is fully mixed with other reaction phases to form multiphase micromixed flow, Multiphase micro-nano flow, multi-phase emulsified flow, multi-phase microstructure 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, Micro foam, micro foam flow, micro gas liquid flow, gas liquid micro nano emulsified flow, ultra micro flow, micro dispersion flow, two micro mixed flow, micro turbulent flow, micro bubble flow, micro bubble, micro bubble flow, micro nano Micro-interface fluid reaction systems such as bubbling and micro-nano bubbling flow; finally enter the inside of the reactor body 1 through the feed port of the reactor body 1, fully react under the action of
  • the reactor main body 1 is used as the main place where the reaction of each reaction raw material in the reaction process occurs, and the whole is a shell structure, which can be specifically: a tank reactor, a tube reactor, and a tower reactor.
  • Fixed bed reactors and fluidized bed reactors as long as the reaction chamber can be used as a multi-phase reaction medium for reaction, to ensure that the multi-phase reaction medium can carry out a sufficient reaction, and the fluidized bed reactor can be based on
  • the different reaction phases in the reaction raw materials can be selected from any type of reactor such as an emulsified bed reactor, a suspended bed reactor, and a fluidized bed reactor.
  • the specific type and structure of the reactor body 1 may be based on chemical engineering, metallurgy, bioengineering, petrochemical engineering, medicine, environmental governance, biochemical fermentation, oil refining, aquaculture, fine chemical industry, biological fermentation, and mineral mining, etc.
  • process parameters such as different application fields, reaction temperature and reaction pressure, as well as the quality requirements of reaction formation, as long as it can ensure that the reaction process can meet the use requirements to the greatest extent, that is, maximize the reaction rate and improve the quality of the finished product. Reduce cost and ensure safe operation.
  • 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 serves as a core device for breaking the gas and/or liquid in the multiphase reaction medium during the reaction process, and is provided with a gas and/or liquid feed port on the reactor body 1 , Passing the gas phase and/or liquid phase in the multiphase reaction medium through mechanical microstructures and/or turbulent microstructures through microchannel action, field force action or mechanical energy action, etc.
  • the mechanical energy of the phase is converted into the surface energy of the gas phase and/or liquid phase, which then breaks the gas phase and/or liquid phase into micron-level micro-bubbles and/or micro-droplets with a diameter of 1 ⁇ m ⁇ de ⁇ 1mm, and interacts with other reaction phases.
  • a microfluidic interface system is formed, which effectively increases the mass transfer area of the phase boundary between the gas and/or liquid phase and the liquid and/or solid phase during the reaction process, and greatly improves the interaction between the reaction phases.
  • the mass transfer efficiency finally realizes the purpose of intensifying the multiple reactions under the lower preset temperature and pressure conditions, and at the same time effectively solves the traditional gas-liquid and gas-liquid-solid multiphase hydrogenation process of high temperature, High pressure, high material consumption, high investment, high safety risk and other issues, thereby significantly reducing equipment investment costs and operating costs.
  • the micro-interface generator 2 is connected to the feed port of the reactor main body 1, and its specific position and quantity can be based on the specific position and the specific position of the gas and/or liquid phase feed port on the reactor main body 1.
  • the quantity is determined, for example, it can be separately installed on the top, bottom or side of the reactor body to form the corresponding top-mounted, bottom-mounted and side-mounted micro-interface strengthening reaction system, or it can be installed at the top and bottom of the reactor body at the same time And the side part to form a variety of opposing micro-interface strengthening reaction systems.
  • 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 multiphase 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 and micro-fluidic method, etc.
  • the field force action method is the use of pressure field, supergravity 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 multi-phase reaction medium required for the reaction enters the reactor body 1 before entering the reactor body 1 to remove the gas and/or gas in the multi-phase reaction medium by means of microchannels, field force or mechanical energy.
  • the liquid is broken into micro-sized bubbles and/or micro-droplets with a diameter of 1 ⁇ m ⁇ de ⁇ 1mm to form micro-interface, micro-nano interface or ultra-micro interface, which effectively increases the gas phase during the reaction And/or the mass transfer area of the phase boundary between the liquid phase and the liquid phase and/or solid phase, thereby increasing the mass transfer efficiency between the reaction phases during the reaction process, and finally reaching the required pressure for the existing enhanced reaction system
  • FIG. 1 it is a kettle-type micro-interface strengthening 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 kettle-type reactor used as a gas -Liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid, and liquid-liquid-solid multiphase reaction medium reaction chamber to ensure that the multiphase reaction medium can fully react
  • the micro-interface generator 2 is connected to the gas-phase inlet and/or liquid-phase inlet on the outer side of the tank reactor, and the number is set to one, which is used for the multiphase reaction medium before entering the tank reactor
  • the gas phase and/or liquid phase in the multi-phase reaction medium are broken into micro-level micro-bubbles and/or micro-droplets with a diameter of 1 ⁇ m ⁇ de ⁇ 1mm in the micro-interface generator 2 by a preset method, and Form a microfluidic interface system with other reaction phases to increase the mass transfer area of
  • the gas-liquid, liquid-liquid, gas-liquid-liquid, liquid-solid, gas-liquid-solid, liquid-liquid-solid and other multiphase media as reaction materials enter the tank reactor Before entering the micro-interface generator 2 through the micro-channel method and the impinging stream breaking method, it is broken into micro-bubbles and/or micro-droplets with a diameter of micrometers, and forms a micro-fluid interface system with other reaction phases, and finally It enters the tank reactor to fully react under the action of the catalyst, and undergoes subsequent treatment to form different reaction products.
  • 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. 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.
  • a tubular micro-interface strengthening reaction system which includes: a reactor main body 1 and a micro-interface generator 2; wherein the reactor main body 1 is a tubular reactor used as a gas -A reaction chamber where the liquid or liquid-liquid two-phase reaction medium is reacted to ensure that the gas-liquid or liquid-liquid two-phase reaction medium can fully react; the micro-interface generator 2 is simultaneously arranged outside the tubular reactor The top gas phase inlet and/or liquid phase inlet and the inside of the tubular reactor are used to remove the gas-liquid or liquid reaction medium before the gas-liquid or liquid-liquid two-phase reaction medium enters the tubular reactor.
  • the gas phase and/or liquid phase in the liquid two-phase reaction medium are broken into micro bubbles and/or micro droplets with a diameter of micrometers in the micro interface generator 2 by a preset method, and form micro bubbles and/or micro droplets with other reaction phases.
  • the gas-liquid or liquid-liquid two-phase reaction medium as the reaction raw material enters the micro-interface generator 2 through the microporous aeration method or impact before entering the tubular reactor.
  • the crushing 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, and finally enters the tubular reactor under the action of the catalyst Fully react and undergo 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 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 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 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 tower reactor for Gas-liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid, and liquid-liquid-solid multiphase reaction medium is reacted in the reaction chamber to ensure that the multiphase reaction medium can fully Reaction; micro-interface generator 2 is connected to the gas inlet and/or liquid phase inlet on the outside of the lower part of the tower reactor, for the multiphase reaction medium before entering the tubular reactor
  • the gas phase and/or liquid phase in the reaction medium are broken into micron-level micro-bubbles and/or micro-droplets with a diameter of 1 ⁇ m ⁇ de ⁇ 1mm in the micro-interface generator 2 by a preset method, and are combined with other reaction phases.
  • a microfluidic interface system is formed to increase the mass transfer area of the phase boundary between the gas and/or liquid phase and the liquid and/or solid phase during the reaction process, and improve the mass transfer efficiency between the reaction phases, thereby achieving The purpose of strengthening the multiple reactions under preset temperature and pressure conditions.
  • the gas-liquid or liquid-liquid two-phase reaction medium as the reaction raw material enters the micro-interface generator 2 through the microporous aeration method, membrane Method (various metal film, inorganic film or organic film), micro channel method, micro fluid control method, pressure field, super gravitational field, ultrasonic field, electromagnetic wave field, impinging stream breaking method, cyclotron shear breaking method, spray method Or one or several methods in the gas-liquid mixed flow pump method are broken into micro bubbles and/or micro droplets with a diameter of micrometers, and form a micro flow interface system with other reaction phases, and finally enter the tower reactor The inside is fully reacted under the action of the catalyst, and then processed to form different reaction products.
  • membrane Method variant metal film, inorganic film or organic film
  • micro channel method micro fluid control method
  • pressure field super gravitational field
  • ultrasonic field ultrasonic field
  • electromagnetic wave field electromagnetic wave field
  • impinging stream breaking method cyclotron shear breaking method
  • spray method Or one or several methods in
  • 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 energy consumption and production cost in the medium reduce the investment intensity, extend 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 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.
  • cobalt-based catalysts and tungsten-based catalysts are examples of cobalt-based catalysts, as long as it can ensure the smooth progress of the strengthening reaction.
  • a fixed-bed micro-interface strengthening 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 for Gas-liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid, and liquid-liquid-solid multiphase reaction medium is reacted in the reaction chamber to ensure that the multiphase reaction medium can fully Reaction; micro-interface generator 2 is respectively arranged in front of the gas inlet and/or liquid phase inlet of the outer top of the fixed bed reactor and inside the fixed bed reactor for entering the multiphase reaction medium into the Before the fixed bed reactor, the gas phase and/or liquid phase in the multiphase reaction medium are broken into micro bubbles and/or micro droplets with a diameter of micrometers in the micro interface generator 2 by a preset method, and Form a microfluidic interface system with other reaction phases to increase the mass transfer area of the phase boundary between the gas and/or liquid phase and the liquid and/or
  • the gas-liquid or liquid-liquid two-phase reaction medium as the reaction raw material enters the micro-interface generator 2 before entering the fixed-bed reactor through microchannel action or mechanical action.
  • microchannel action or mechanical action Broken into micron-level micro-bubbles and/or micro-droplets with a diameter of 1 ⁇ m ⁇ de ⁇ 1mm, and form a microfluidic interface system with other reaction phases, and finally enter the fixed-bed reactor to fully react under the action of the catalyst , And subsequent processing to form different reaction products.
  • 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.
  • an emulsion bed micro-interface strengthening reaction system which includes: a reactor body 1 and a micro-interface generator 2; wherein the reactor body 1 is an emulsion bed reactor for Gas-liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid, and liquid-liquid-solid multiphase reaction medium is reacted in the reaction chamber to ensure that the multiphase reaction medium can fully Reaction; 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 number is two, one of which is set outside the emulsified bed reactor, and the other is set at The inside of the emulsion bed reactor is used to pass the gas phase and/or liquid phase in the multiphase reaction medium through the micro-interface generator 2 before the multiphase reaction medium enters the emulsion bed reactor
  • the preset method breaks into micro-sized bubbles and/or micro-droplets with a diameter of 1
  • the gas-liquid or liquid-liquid two-phase reaction medium as the reaction raw material enters the micro-interface generator 2 before entering the emulsion bed reactor through mechanical action and field force action. It is broken 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 emulsified bed reactor to fully react under the action of the catalyst, and undergoes subsequent treatment to Different reaction products are formed.
  • 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.
  • 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 strengthening 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 for Gas-liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid, and liquid-liquid-solid multiphase reaction medium is reacted in the reaction chamber to ensure that the multiphase reaction medium can fully Reaction; micro-interface generator 2 is connected to the bottom end of the suspended bed reactor and the side gas inlet and/or liquid phase inlet, the number of which is set to two, wherein the side micro-interface generator 2 is connected to On the outside of the suspended bed reactor, the micro-interface generator 2 at the bottom end is connected to the inside of the suspended bed reactor, and at the same time is used to remove the multiphase reaction medium before entering the suspended bed reactor.
  • the reactor body 1 is a suspended bed reactor for Gas-liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid, and
  • the gas phase and/or liquid phase in the reaction medium are broken into micron-level micro-bubbles and/or micro-droplets with a diameter of 1 ⁇ m ⁇ de ⁇ 1mm in the micro-interface generator 2 by a preset method, and are combined with other reaction phases.
  • a microfluidic interface system is formed to increase the mass transfer area of the phase boundary between the gas and/or liquid phase and the liquid and/or solid phase during the reaction process, and improve the mass transfer efficiency between the reaction phases, thereby achieving The purpose of strengthening the multiple reactions under preset temperature and pressure conditions.
  • the gas-liquid or liquid-liquid two-phase reaction medium used as the reaction material before entering the suspended bed reactor, the gas-liquid or liquid-liquid two-phase reaction medium used as the reaction material first enters the micro-interface generator 2 through microchannel action and field force.
  • 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 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 for Gas-liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid, and liquid-liquid-solid multiphase reaction medium is reacted in the reaction chamber to ensure that the multiphase reaction medium can fully The reaction; the micro-interface generator 2 is connected to the gas-phase inlet and/or the liquid-phase inlet at the bottom and the side of the fluidized bed reactor, the number of which is set to two, wherein the micro-interface generator 2 on the side is connected to Inside the suspended bed reactor, the micro-interface generator 2 at the bottom end is connected to the outside of the suspended bed reactor, and at the same time is used to convert the multiphase reaction medium into the ebullating bed reactor.
  • the reactor body 1 is a fluidized bed reactor for Gas-liquid, liquid-liquid, liquid-solid, gas-liquid
  • the gas phase and/or liquid phase in the reaction medium are broken into micron-level micro-bubbles and/or micro-droplets with a diameter of 1 ⁇ m ⁇ de ⁇ 1mm in the micro-interface generator 2 by a preset method, and are combined with other reaction phases.
  • a microfluidic interface system is formed to increase the mass transfer area of the phase boundary between the gas and/or liquid phase and the liquid and/or solid phase during the reaction process, and improve the mass transfer efficiency between the reaction phases, thereby achieving The purpose of strengthening the multiple reactions under preset temperature and pressure conditions.
  • the gas-liquid or liquid-liquid two-phase reaction medium as the reaction raw material enters the micro-interface generator 2 before entering the fluidized bed reactor through the action of microchannels and field forces.
  • 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, extend the equipment operation cycle, ensure the poor intrinsic safety of 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 be used in various hydrogenation reactions, oxidation reactions, chlorination reactions, carbonylation reactions and combustible ice mining and other reaction processes to form micro-interfaces, micro-nano interfaces, ultra-micro interfaces, and micro-bubble biochemical processes.
  • microbubble bioreactor 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 , Microbubble oxygenation, 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-structure flow, gas-liquid-solid micro-mixed flow, gas-liquid-solid micro Nanoflow, gas-liquid-solid emulsified flow, gas-liquid-solid microstructure flow, microbubble, microbubble flow, microbubble, microbubble flow, micro-gas-liquid flow, gas-liquid micro-nano emulsion flow, ultra-micro flow, micro-dispersion flow, Two types of microfluid, such as micro-mixed flow, micro-turbulent flow, micro-bubble flow, micro-bubble, micro-bubble flow, micro-nano bubble and micro
  • the micro-interface strengthening reaction system provided by the present invention, by connecting the micro-interface generator to the reactor main body, generates the gas and/or liquid in the multi-phase reaction medium at the micro-interface before the multi-phase reaction medium enters the reactor main body.
  • the vessel is broken into micro-bubbles and/or micro-droplets with a diameter of micrometers through micro-channels, field forces or mechanical energy, effectively increasing the gas, liquid and/or gas, liquid and solid phases during the reaction process
  • the mass transfer area between the phase boundaries greatly enhances the mass transfer efficiency of each reaction phase in the reaction process, and further achieves the purpose of strengthening the reaction within the preset pressure range.
  • micro-interface strengthening reaction system provided by the present invention
  • different micro-interface generators can be selected according to the characteristics of different reaction phases and process requirements, and then different crushing methods, such as microchannels, field forces, or
  • the action of mechanical energy breaks the gas and/or liquid in the reaction medium, which effectively ensures the effectiveness of the gas and/or liquid in the reaction medium before the multiphase reaction medium enters the main body of the reactor, and ensures the gas phase in the reaction process
  • the mass transfer efficiency of the phase boundary between the liquid phase and/or gas phase, liquid phase and solid phase further improves the reaction efficiency.

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Abstract

L'invention concerne un système de réaction amélioré par micro-interface, comprenant : un corps principal de réacteur (1), qui agit comme une chambre de réaction pour la réaction d'un milieu réactionnel multiphase gaz-liquide, liquide-liquide, liquide-liquide-solide, liquide-solide ou gaz-liquide-solide ; et un générateur de micro-interface (2), relié au corps principal de réacteur (1), pour broyer la phase gazeuse et/ou la phase liquide dans le milieu réactionnel multiphase en microbulles et/ou microgouttelettes ayant un diamètre d'échelle micrométrique d'une manière prédéfinie dans le générateur de micro-interface (2) avant que le milieu réactionnel multiphase ne pénètre dans le corps principal de réacteur (1).
PCT/CN2019/090253 2019-03-15 2019-06-06 Système de réaction amélioré par micro-interface WO2020186633A1 (fr)

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CN113908787A (zh) * 2021-11-19 2022-01-11 西安交通大学 一种微反应通道结构及基于其的声学微反应器和化工生产系统
CN115041110A (zh) * 2022-06-20 2022-09-13 浙江大学 一种液-液非均相反应强化方法及装置
CN115155479B (zh) * 2022-07-12 2023-11-21 南京工业大学 一种多级进料微界面强化传质反应器

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