DE212019000177U1 - Microinterfacial enhanced hydrogenation reaction system - Google Patents

Abstract

Microinterface-enhanced hydrogenation reaction system characterized in that it comprises
a reactor body serving as a reaction chamber in the hydrogenation reaction process to ensure that the hydrogenation reaction can sufficiently proceed;
a micro-interface generator, which is connected to the reactor body, so that before the hydrogen enters the hydrogenation reaction process with a liquid and / or a solid-liquid mixture into the reactor body, the hydrogen and / or the liquid reactant in the micro-interface generator by means of a mechanical microstructure and / or a turbulent microstructure in a predetermined mode of action into which microbubbles and / or microdroplets with a diameter in the micrometer range are comminuted in order to increase the phase boundary mass transfer surface between the hydrogen and the liquid and / or solid-liquid mixture in the course of the reaction, wherein the mass transfer efficiency between the reaction phases is increased and the hydrogenation reaction rate is improved at a given temperature and under a given pressure.

Description

TECHNICAL AREA

The present utility model belongs to the technical field of reaction improvement, particularly relates to a micro-interface-enhanced hydrogenation reaction system.

STATE OF THE ART

Gas-liquid reaction processes such as gas-liquid, gas-liquid-solid and the like are widely used in the fields of energy, petrochemicals and fine chemicals and the like. Gas-liquid multiphase reactions, such as oxidation, hydrogenation, chlorination and the like, have macroscopic reaction rates that are generally limited by the mass transfer process. The volumetric mass transfer coefficient of the gas-liquid reaction is mainly influenced by the mass transfer coefficient and the area of the gas-liquid phase boundary. Investigations have shown that the phase boundary area has a great influence on the volumetric mass transfer coefficient and is easily controllable. Therefore, increasing the interface area is believed to be an effective way to increase the rate of the macroscopic gas-liquid reaction. Bubble reactors and stirred-bubble reactors are currently common gas-liquid reactors. For example, tower-shaped bubble reactors, in which a TA is produced by oxidizing PX, often have bubble diameters of more than 3mm to even centimeters, and have a limited mass transfer interface. In order to increase the macroscopic rate of reaction, it is necessary to promote liquid turbulence by increasing the amount of ventilation, which increases the breakage of bubbles to increase the number of bubbles and thereby increase the interface. This inevitably leads to a lower gas utilization, an increased compressor output and increased exhaust gas emissions, to an excessive energy consumption and to a loss of material and to environmental pollution. Stirring-bubble gas-liquid reactors often form large eddies that affect the macroscopic movement of bubbles, but have little effect on the breaking of bubbles, the bubbles are not crushed efficiently and therefore the diameter is large and the Mass transfer area is limited, so that the reaction efficiency is low. In order to enhance the gas-liquid mass transfer, internals such as tower plates, static mixers and the like are generally added inside the column to improve mixing, and the stirred tank is provided with structures such as stirring blades or inner tubes with different structures around the To increase the gas content of the liquid layer. In the two reactors, the phase boundary area provided and the mass transfer coefficient (liquid side, gas side, solid-liquid) are limited, which due to the resulting bubble diameter of in general 3 to 30mm, so that it is difficult to achieve a breakthrough improvement in response performance.

CONTENTS OF THE PRESENT USED MODEL

In view of this fact, according to the present utility model, a microinterfacial-enhanced hydrogenation reaction system is proposed which solves the problems in which the previous hydrogenation reaction intensification systems pose challenges to industrialized mass production in carrying out the reaction amplification, with the increase in the phase boundary area of the in carrying out the reaction amplification respective reaction phase takes place through high temperatures and pressures, which in turn leads to high energy consumption and high production costs, high investment stability, short device operating cycle, high number of failures, poor intrinsic safety and the like with an increased mass transfer rate.

• einen Reaktorkörper, der als Reaktionskammer in dem Hydrierungsreaktionsprozess dient, um sicherzustellen, dass die Hydrierungsreaktion ausreichend fortschreiten kann;
• einen Mikrogrenzflächengenerator (Micro Interfacial Generator, kurz MIG), der mit dem Reaktorkörper verbunden ist, damit vor dem Eintritt des Wasserstoffs im Hydrierungsreaktionsprozess mit einer Flüssigkeit und/oder einem Festkörper-Flüssigkeit-Mischgut in den Reaktorkörper der Wasserstoff und/oder der flüssige Reaktant in dem Mikrogrenzflächengenerator mittels einer mechanischen Mikrostruktur und/oder einer turbulenten Mikrostruktur in einer vorbestimmten Wirkungsweise in die Mikroblasen und/oder Mikrotröpfchen mit einem Durchmesser im Mikrometerbereich zerkleinert werden, um die Phasengrenze-Stoffübertragungsfläche zwischen dem Wasserstoff und der Flüssigkeit und/oder Festkörper-Flüssigkeit-Mischgut im Verlauf der Reaktion zu vergrößern, wobei der Stoffübertragungswirkungsgrad zwischen den Reaktionsphasen vergrößert und die Reaktionshydrierungsreaktionsrate bei vorgegebener Temperatur und unter vorgegebenem Druck verbessert wird.

The present utility model provides a micro-interface-enhanced hydrogenation reaction system which comprises:

• a reactor body serving as a reaction chamber in the hydrogenation reaction process to ensure that the hydrogenation reaction can sufficiently proceed;
• a micro interfacial generator (MIG for short), which is connected to the reactor body, so that the hydrogen and / or the liquid reactant in the reactor body before the entry of hydrogen in the hydrogenation reaction process with a liquid and / or a solid-liquid mixture the micro-boundary surface generator by means of a mechanical microstructure and / or a turbulent microstructure in a predetermined mode of action into which micro-bubbles and / or microdroplets with a diameter in the micrometer range are comminuted to create the phase boundary mass transfer surface between the hydrogen and the liquid and / or solid-liquid mixture to increase in the course of the reaction, the mass transfer efficiency between the reaction phases and the reaction hydrogenation reaction rate is improved at a given temperature and under a given pressure.

In a further development it is provided that in the above-described micro-interface-enhanced hydrogenation reaction system, the predetermined mode of action is selected from one or more of the microchannel mode of action, the field force mode of action and the mechanical energy action; in which
the microchannel action by forming a microstructure of the flow channel breaks up the gas phase and / or liquid phase passing through the microflow channel into the microbubbles and / or microdroplets;
wherein the field force action by an external field force action supplies the energy into the liquid in a non-contact manner to break it up into the microbubbles or microdroplets;
the mechanical energy action by the mechanical energy in the liquid converts it into a surface energy of the bubbles or droplets so that the bubbles or droplets are broken into the microbubbles or microdroplets.

In a further development, it is provided that in the above-described micro-interface-enhanced hydrogenation reaction system, the microchannel mode of action is selected from one or more of a microporous ventilation method, a micronanoporous membrane method, a microflow channel method and a microfluidic method.

In a further development, it is provided that in the above-described micro-interface-enhanced hydrogenation reaction system, the field force action comprises a pressure field effect, a supergravity field effect, an ultrasonic field effect or an electromagnetic wave field effect.

In a further development it is provided that in the above-described micro-interface-enhanced hydrogenation reaction system, the mechanical energy action comprises an impact flow fracture method, a vortex shear fracture method, a spray method or a gas-liquid mixed flow pump method.

In a further development it is provided that in the above-described micro-interface-enhanced hydrogenation reaction system, the reactor body comprises a tank reactor, a tubular reactor, a tower reactor, a fixed bed reactor or a fluidized bed reactor.

In a further development it is provided that in the above-described micro-interface-enhanced hydrogenation reaction system, the micro-interface generator is connected to the gas phase and / or liquid phase inlet end of the reactor body, the number of which is provided as at least one group.

In a further development it is provided that in the above-described micro-interface-enhanced hydrogenation reaction system, the preset pressure range is between 10% and 80% of the pressure required for reactions in the existing hydrogenation reaction-enhancing systems.

In a further development, it is provided that in the above-described micro-interface-enhanced hydrogenation reaction system, the area on the order of micrometers is greater than or equal to 1 μm and less than 1 mm.

In a further development it is provided that in the above-described micro-interface-enhanced hydrogenation reaction system, the micro-interface-enhanced hydrogenation reaction system in hydrogenation reactions in the fields of the chemical industry, metallurgy, biotechnology, petroleum work, medicine, environmental treatment, biochemical fermentation, the Refineries, aquaculture, fine chemistry, bio-fermentation and mineral mining can be used.

The advantages of the utility model over the prior art are that in a micro-interface-enhanced hydrogenation reaction system provided by the present utility model, a micro-interface generator is connected to the reactor body, so that before the hydrogen enters the hydrogenation reaction process with a liquid and / or a solid-liquid- Mixture in the reactor body, the hydrogen and / or the liquid reactant in the micro-boundary surface generator by means of a mechanical microstructure and / or a turbulent microstructure in a predetermined mode of action in the microbubbles and / or microdroplets with a diameter in the micrometer range are comminuted, so that the phase boundary-mass transfer surface between the hydrogen and the liquid and / or the solid-liquid mixture is effectively increased in the course of the reaction, whereby the mass transfer efficiency between the reaction phases increases I is improved, further achieving the goal of amplifying the reaction in a lower predefined pressure range, while drastically reducing energy consumption and production costs during the reaction, reducing investment, extending the service life of the plant, a poor intrinsic safety is ensured during the reaction, which effectively ensures the industrial mass production of the reaction products.

In particular, in the micro-interface-enhanced hydrogenation reaction system that is provided by the present utility model, the selection of different types of comminution can be made according to the properties of the different reaction phases and the process requirements, such as the comminution of gases and / or liquids in the reaction medium through microchannels , Field or mechanical energy effect, which effectively ensures the effectiveness of the comminution of gases and / or liquids in a reaction medium before the entry of the reaction medium into the reactor body during the hydrogenation, whereby the phase boundary mass transfer efficiency in the gas phase, in the liquid phase and / or ensured between the gaseous phase, the liquid phase and the solid phase in the course of the reaction, whereby the reaction efficiency is further increased.

Figure list

• 1 eine schematische Darstellung der Struktur des tankförmigen Mikrogrenzflächen-verstärkten Hydrierungsreaktionssystems eines Ausführungsbeispiels des vorliegenden Gebrauchsmusters;
• 2 eine schematische Darstellung der Struktur des rohrförmigen Mikrogrenzflächen-verstärkten Hydrierungsreaktionssystems eines Ausführungsbeispiels des vorliegenden Gebrauchsmusters;
• 3 eine schematische Darstellung der Struktur des turmartigen Mikrogrenzflächen-verstärkten Hydrierungsreaktionssystems eines Ausführungsbeispiels des vorliegenden Gebrauchsmusters;
• 4 eine schematische Darstellung der Struktur des Festbett-Mikrogrenzflächen-verstärkten Hydrierungsreaktionssystems eines Ausführungsbeispiels des vorliegenden Gebrauchsmusters;
• 5 eine schematische Darstellung der Struktur des Emulgierbett-Mikrogrenzflächen-verstärkten Hydrierungsreaktionssystems eines Ausführungsbeispiels des vorliegenden Gebrauchsmusters;
• 6 eine schematische Darstellung der Struktur des Suspensionsbett-Mikrogrenzflächen-verstärkten Hydrierungsreaktionssystems eines Ausführungsbeispiels des vorliegenden Gebrauchsmusters;
• 7 eine schematische Darstellung der Struktur des Siedebett-Mikrogrenzflächen-verstärkten Hydrierungsreaktionssystems eines Ausführungsbeispiels des vorliegenden Gebrauchsmusters.

Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of a preferred embodiment. The drawings only serve the purpose of illustrating preferred embodiments and are not to be understood as a restriction of the present utility model. In addition, the same reference numbers will be used throughout the drawings to refer to the same elements. In the drawings shows

• 1 Fig. 3 is a schematic diagram showing the structure of the tank-shaped micro-interface-enhanced hydrogenation reaction system of an embodiment of the present utility model;
• 2 Fig. 3 is a schematic representation of the structure of the tubular micro-interface-enhanced hydrogenation reaction system of an embodiment of the present utility model;
• 3 Fig. 3 is a schematic representation of the structure of the tower-like micro-interface-enhanced hydrogenation reaction system of an embodiment of the present utility model;
• 4th Fig. 3 is a schematic diagram showing the structure of the fixed bed micro-interface enhanced hydrogenation reaction system of an embodiment of the present utility model;
• 5 Fig. 13 is a schematic diagram showing the structure of the emulsification bed microinterfacial enhanced hydrogenation reaction system of an embodiment of the present utility model;
• 6th Fig. 3 is a schematic representation of the structure of the suspension bed microinterfacial enhanced hydrogenation reaction system of an embodiment of the present utility model;
• 7th Fig. 3 is a schematic representation of the structure of the boiling bed microinterfacial enhanced hydrogenation reaction system of an embodiment of the present utility model.

DETAILED DESCRIPTION

The technical solutions in the exemplary embodiments for the utility model are described clearly and completely below with the accompanying figures in the exemplary embodiments for the utility model. Obviously, the exemplary embodiment described is only part and not all of the exemplary embodiments of the utility model. All other exemplary embodiments that are obtained by those of ordinary skill in the art based on the exemplary embodiments of the present utility model without creative effort are intended to fall within the scope of the present utility model.

With reference to the 1 to 7th there is shown a microinterfacial enhanced hydrogenation reaction system of an embodiment of the present utility model which includes a reactor body 1 and a micro-interface generator 2 includes; being the reactor body 1 serves as a reaction chamber in the hydrogenation reaction process to ensure that the hydrogenation reaction can sufficiently proceed; where the micro-boundary generator 2 with the reactor body 1 is connected, wherein before the entry of the hydrogen in the hydrogenation reaction process with a liquid and / or a solid-liquid mixture in the reactor body, the hydrogen and / or the liquid reactant in the micro-interface generator by means of a mechanical microstructure and / or a turbulent microstructure in a predetermined Mode of action into which microbubbles and / or microdroplets with a diameter in the micrometer range are comminuted to form a micro-interface, a micro-nano-interface, an ultra-micro-interface or the like in other reaction phases and together with other reaction phases to form a multiphase micromixing flow , a multi-phase micro-nano-flow, a multi-phase emulsification flow, a Multiphase microstructure flow, a gas-liquid-solid-micro-mixed flow, a gas-liquid-solid-micro-nano-flow, a gas-liquid-solid-solid-emulsate flow, a gas-liquid-solid-microstructure flow, a microbubble , a microbubble flow, a micro-foam, a micro-foam flow, a micro-gas-liquid flow, a gas-liquid-micro-nanoemulsion flow, an ultra-micro-flow, a micro-dispersion flow, a two-phase micro-mixing flow, a micro-turbulence flow, a micro-bubble flow, a Microbubble, a microbubble flow, a micro-nanobubble and a micro-nanobubble flow, and other multiphase liquids formed by micron-sized particles or multiphase liquids formed by micro-nano-scale particles (referred to as micro-interfacial liquid for short referred to), whereby the phase boundary mass transfer surface between the gas phase and / o that of the liquid phase and the liquid phase and / or the solid phase is validly increased in the course of the hydrogenation, and the mass transfer efficiency between the hydrogen and the respective reaction phases is increased significantly, which finally achieves the goal of the hydrogenation reaction under lower preset temperature and temperature To improve pressure conditions while at the same time effectively solving the problems such as high temperature, high pressure, high material consumption, high investment, high safety risk in conventional hydrogenation reaction processes, thereby significantly reducing the investment and operating costs of the plant.

In the present exemplary embodiment it is provided that the hydrogen and another medium with different phases than the reaction raw material before entering the reactor body 1 into the micro-boundary generator 2 occur, wherein the liquid and / or the hydrogen during the hydrogenation reaction in the microbubbles and / or microdroplets with a diameter in the micrometer range are crushed by the mechanical and / or turbulent microstructure inside the micro-interface generator into microchannel effects, field force effects or mechanical energy effects or the like, wherein a micro-interface, a micro-nano-interface, or an ultra-micro-interface or the like is formed; then mixed with other reaction phases to form a multiphase micromixing flow, a multiphase micro-nano-flow, a multiphase emulsification flow, a multiphase microstructure flow, a gas-liquid-solid-micro-mixed flow, a gas-liquid-solid -Micro-nano-flow, a gas-liquid-solid-solid-emulsified flow, a gas-liquid-solid microstructure flow, a microbubble, a microbubble flow, a microfoam, a microfoam flow, a micro-gas-liquid flow, a gas-liquid -Micro-nanoemulsion flow, an ultra-micro-flow, a micro-dispersion flow, a two-component micromixing flow, a microturbulence flow, a microbubble flow, a microbubble, a microbubble flow, a micro-nanobubble and a micro-nanobubble flow, and other micro-interface liquid reaction systems ; finally through the inlet opening of the reactor body 1 into the interior of the reactor body 1 be fully reacted with the aid of a catalyst, and subsequently processed to form different reaction products, whereby the phase boundary mass transfer area between the hydrogen and / or the liquid phase and the liquid phase and / or the solid phase is validly enlarged in the course of the reaction, whereby the Mass transfer efficiency between the hydrogen and the respective reaction phases in the hydrogenation reaction process is increased, ultimately achieving the goal of increasing the hydrogenation reaction in the range of 10% -80% of the pressure required for the reaction in the existing reaction enhancement system; at the same time the problems such as high temperature, high pressure, high material consumption, high investment, high safety risk in conventional hydrogenation reaction processes are effectively solved, whereby the investment and operating costs of the plant are considerably reduced.

Specifically, it is provided that the reactor body 1 is used as the main place where each reaction raw material reacts in the hydrogenation reaction process, and its whole is a shell structure which can be specific: a tank reactor, a tubular reactor, a tower reactor, a fixed bed reactor and a fluidized bed reactor as long as it can serve as a reaction chamber of a hydrogenation reaction, to ensure that the hydrogenation reaction can proceed to completion, the fluidized bed reactor in turn being any reactor selected after the various reaction phases in the reaction raw material, such as an emulsifying bed reactor, a suspension bed reactor, a boiling bed reactor or the like.

In the present embodiment, it is provided that the specific type and configuration of the reactor body 1 selected and designed on the basis of various application areas, such as chemical industry, metallurgy, biotechnology, petrochemistry, medicine, environment and biochemistry, as well as process parameters such as reaction temperatures and reaction pressure, as well as parameters such as quality requirements for reaction products as long as it can be ensured that the usage requirements in the reaction process can be met to the maximum, ie a maximum increase in the reaction speed, an increase in product quality, a reduction in costs and a guarantee of safe operation. It goes without saying that the specific configurations of the reactor body 1 Inevitably differ to a certain extent in different areas or different reaction processes, for example with regard to the arrangement and number of inputs and outputs. Outlet openings.

Specifically, it is provided that the micro-interface generator 2 serves as a core device for cracked gases and / or liquids in a hydrogenation reaction process, in which an inlet opening for gaseous and / or liquid phases on the reactor body 1 is arranged, wherein the gas phase and / or the liquid phase in the hydrogenation reaction process through the mechanical microstructure and / or the turbulent microstructure in microchannel effect, field force effect or mechanical energy effect or the like, the mechanical energy of the gas phase and / or the liquid phase in the hydrogenation reaction process into the surface energy of the gas phase and / or converts the liquid phase, whereby the gas phase and / or the liquid phase are further comminuted to micro-bubbles and / or microdroplets in the micrometer range with a diameter between 1 and 1000 µm and form a microfluidic interface system with the other reaction phases, whereby the phase boundary mass transfer surface between the Gas phase and / or the liquid phase and the liquid phase and / or the solid phase in the hydrogenation reaction process is validly enlarged, whereby the mass transfer efficiency between the individual reaction phases is considerably improved d ultimately the task of enhancing the hydrogenation reaction at lower temperatures and pressures is solved, while at the same time the problems such as high temperature, high pressure, high material consumption, high investment, high safety risk in conventional hydrogenation reaction processes are effectively solved, whereby the Investment and operating costs of the plant can be reduced considerably.

In the present embodiment it is provided that the micro-boundary surface generator 2 in front of the inlet opening of the reactor body 1 is connected upstream, its specific position and number according to the specific location and number of input openings for the gaseous and / or liquid phase on the reactor body 1 can be determined, wherein the microinterface generator can be arranged separately, for example, on the top, the bottom or the side of the reactor to form corresponding top-mounted, bottom-mounted and side-mounted micro-interface-enhanced hydrogenation reaction systems, the micro-interface generator also simultaneously top, bottom and can be positioned on the sides of the reactor to form a variety of counteracting microinterfacial enhanced hydrogenation reaction systems. At the same time is the micro-interface generator 2 inside and / or outside of the reactor body 1 arranged. In particular, it is provided that the specific way in which the micro-interface generator fragments the gaseous and / or liquid phases in the hydrogenation reaction can also be selected from one or a combination of several of the microchannel mode of action, the field force mode of action and the mechanical energy mode of action according to the specific process requirements; wherein the microchannel mode of action breaks up the gas phase and / or liquid phase passing through the microflow channel into the microbubbles and / or microdroplets by forming a microstructure of the flow channel, the microchannel mode of action, for example, a microporous ventilation process, a micronanoporous membrane process (different types of metallic, inorganic or organic membranes) , a microflow channel method or a microfluidic method and the like; wherein the field force action by an external field force action such as a pressure field, an ultra-gravity field, an ultrasound field or an electromagnetic wave field to supply the energy into the liquid in a non-contact manner to break it down into the microbubbles or microdroplets; whereby the mechanical energy action by the mechanical energy in the liquid converts it into a surface energy of the bubbles or droplets so that the bubbles or droplets are broken into the microbubbles or microdroplets, the mechanical energy action an impact flow fracture method, a vortex shear fracture method, a spray method and a gas-liquid mixed flow pumping method or the like. During use, the hydrogen required for the reaction reaches the reactor body with other reaction media before it enters the reactor 1 inside, the gas and / or the liquid during the hydrogenation reaction in the microbubbles and / or microdroplets in the micrometer range with a diameter of 1µm≤de <1mm by the microchannel effects, field force effects or mechanical energy effects or the like are comminuted to create a micro interface, to form a micro-nano-interface or an ultra-micro-interface or the like; whereby the phase boundary mass transfer area between the gas phase and / or the liquid phase and the liquid phase and / or the solid phase in the hydrogenation reaction process is validly increased, whereby the The mass transfer efficiency between the respective reaction phases is increased in the course of the reaction, thereby ultimately achieving the goal of increasing the hydrogenation reaction in the range of 10% -80% of the pressure required for the reaction in the existing reaction enhancement system; at the same time the problems such as high temperature, high pressure, high material consumption, high investment, high safety risk in conventional hydrogenation reaction processes are effectively solved, whereby the investment and operating costs of the plant are considerably reduced.

With reference to the 1 Also shown is a microinterfacial enhanced hydrogenation reaction system of an embodiment of the present utility model which includes a reactor body 1 and a micro-interface generator 2 includes; being the reactor body 1 is a tank reactor that serves as a reaction chamber in the hydrogenation reaction to ensure that the hydrogenation reaction can sufficiently proceed; being a micro-boundary generator 2 is connected to the gas phase inlet and / or the liquid phase inlet on the outside of the tank reactor, the number of which is provided at one, so that before the entry of the hydrogen in the hydrogenation reaction process with a liquid and / or a solid-liquid mixture into the reactor body, the hydrogen and / or the liquid reactant in the micro-interface generator is comminuted into the micro-bubbles and / or microdroplets in the micrometer range with a diameter of 1 µm≤de <1mm by means of a predetermined process and form a microfluid interface system with other reaction phases in order to create the phase boundary-mass transfer surface between the gas phase and / or to enlarge the liquid phase and the liquid phase and / or the solid phase in the hydrogenation reaction process, the mass transfer efficiency between the respective reaction phases being increased and the aim of enhancing the hydrogenation reaction at a given temperature and below r given pressure is reached. In the present exemplary embodiment, the hydrogen and the liquid and / or the solid-liquid mixture as the reaction raw material are first fed into the micro-interface generator before entering the tank reactor 2 occur, through the micro flow channel process and the impingement flow rupture process into the microbubbles and / or microdroplets with a diameter in the micrometer range, and form a microfluidic interface system with other reaction phases, and finally enter the interior of the tank reactor, are reacted with the aid of a catalyst , and subsequently processed to form different reaction products. While using this system: 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 drastically reduces the energy consumption and production cost during the reaction, reducing the investment strength , the service life of the plant is extended, poor intrinsic safety is ensured during the reaction, which effectively ensures the industrial mass production of the reaction products. It goes without saying that this reaction in the present embodiment is a type of reaction in which a tank reactor is used for reaction enhancement so that the type of catalyst is not particularly limited, which is one or a combination of an iron-based catalyst, a Molybdenum-based catalyst, a nickel-based catalyst, a cobalt-based catalyst and a tungsten-based catalyst can act as long as it can be ensured that the amplification reaction proceeds smoothly.

With reference to the 2 Also shown is a tubular microinterfacial enhanced hydrogenation reaction system of an embodiment of the present utility model, which includes a reactor body 1 and a micro-interface generator 2 includes; being the reactor body 1 is a tubular reactor that serves as a reaction chamber in the hydrogenation reaction to ensure that the hydrogenation reaction can sufficiently proceed; where the micro-boundary generator 2 is arranged at the same time in front of the gas phase inlet and / or the liquid phase inlet at the outer upper end of the tubular reactor and in the interior of the tubular reactor, so that before the entry of the hydrogen in the hydrogenation reaction process with a liquid and / or a solid-liquid mixture into the reactor body, the hydrogen and / or the liquid reactant in the micro-interface generator 2 using a predetermined process into which microbubbles and / or microdroplets in the micrometer range with a diameter of 1µm≤de <1mm are comminuted and form a microfluidic interface system with other reaction phases to form the phase boundary - mass transfer surface between the gas phase and / or the liquid phase and the liquid phase and / or to enlarge the solid phase in the hydrogenation reaction process, the mass transfer efficiency between the respective reaction phases being increased and thereby the aim of enhancing the hydrogenation reaction at a given temperature and under a given pressure is achieved. Specifically, the hydrogen and the liquid and / or the solid-liquid mixture as the reaction raw material are in the present exemplary embodiment first of all into the micro-interface generator before entering the tubular reactor 2 occur, through the microporous ventilation process or the impingement flow rupture into the microbubbles and / or microdroplets with a diameter in the micrometer range, and form a microfluidic interface system with other reaction phases, and finally enter the interior of the tubular reactor, are reacted with the aid of a catalyst, and subsequently processed to form different reaction products. While using this system: the reaction pressure in the tubular reactor is 30% -70% of the internal pressure of the existing tubular reactor and the reaction temperature is 91% -94% of the existing reaction temperature, which drastically reduces the energy consumption and the production cost during the reaction, reduces the investment strength , the service life of the plant is extended, poor intrinsic safety is ensured during the reaction, which effectively ensures the industrial mass production of the reaction products. It goes without saying that this reaction in the present embodiment is a type of reaction in which a tubular reactor is used for reaction enhancement so that the type of catalyst is not particularly limited, which is one or a combination of an iron-based catalyst, a Molybdenum-based catalyst, a nickel-based catalyst, a cobalt-based catalyst and a tungsten-based catalyst can act as long as it can be ensured that the amplification reaction proceeds smoothly.

With reference to the 3 there is further shown a tower-shaped microinterfacial-enhanced hydrogenation reaction system of an embodiment of the present utility model which has a reactor body 1 and a micro-interface generator 2 includes; being the reactor body 1 is a tower reactor that serves as a reaction chamber in the hydrogenation reaction to ensure that the hydrogenation proceeds sufficiently; where the micro-boundary generator 2 of the gas phase inlet and / or the liquid phase inlet is connected to the outside of the lower part of the tower reactor, so that before the entry of the hydrogen in the hydrogenation reaction process with a liquid and / or a solid-liquid mixture into the reactor body, the hydrogen and / or the liquid reactant in the micro-boundary generator 2 using a predetermined process into which microbubbles and / or microdroplets in the micrometer range with a diameter of 1µm≤de <1mm are comminuted and form a microfluidic interface system with other reaction phases to form the phase boundary - mass transfer surface between the gas phase and / or the liquid phase and the liquid phase and / or to enlarge the solid phase in the hydrogenation reaction process, the mass transfer efficiency between the respective reaction phases being increased and thereby the aim of enhancing the hydrogenation reaction at a given temperature and under a given pressure is achieved. Specifically, the hydrogen and the liquid and / or the solid-liquid mixture as the raw material for the reaction in the present exemplary embodiment are first introduced into the micro-interface generator before entering the tower reactor 2 occur, by one or more of the microporous ventilation process, the micro flow channel process, the microfluidic process, the pressure field, the ultra-gravity field, the ultrasonic field, the electromagnetic wave field, the impact flow fracture method, the vortex shear fracture method, the spray method or the gas Liquid mixed flow pumping processes in which microbubbles and / or microdroplets with a diameter in the micrometer range are crushed, and form a microfluidic interface system with other reaction phases, and finally enter the interior of the tower reactor, are fully reacted with the aid of a catalyst, and are subsequently processed to form different reaction products . While using this system: 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 drastically reduces the energy consumption and production cost during the reaction, reduces the investment strength , the service life of the plant is extended, poor intrinsic safety is ensured during the reaction, which effectively ensures the industrial mass production of the reaction products. It goes without saying that this reaction in the present embodiment is a type of reaction in which a tower reactor is used for reaction enhancement so that the type of catalyst is not particularly limited, which is one or a combination of an iron-based catalyst, a Molybdenum-based catalyst, a nickel-based catalyst, a cobalt-based catalyst and a tungsten-based catalyst can act as long as it can be ensured that the amplification reaction proceeds smoothly.

With reference to the 4th Also shown is a fixed bed microinterfacial enhanced hydrogenation reaction system of an embodiment of the present utility model which includes a reactor body 1 and a micro-interface generator 2 includes; being the reactor body 1 is a fixed bed reactor that serves as a reaction chamber in the hydrogenation reaction to ensure that the hydrogenation reaction can sufficiently proceed; where the micro-boundary generator 2 in each case before the gas phase inlet and / or the Liquid phase inlet is arranged at the outer upper end of the fixed bed reactor and inside the fixed bed reactor, so that before the entry of the hydrogen in the hydrogenation reaction process with a liquid and / or a solid-liquid mixture into the reactor body, the hydrogen and / or the liquid reactant in the micro-interface generator by means of a predetermined method into which microbubbles and / or microdroplets in the micrometer range are comminuted with a diameter and form a microfluidic interface system with other reaction phases to form the phase boundary mass transfer surface between the gas phase and / or the liquid phase and the liquid phase and / or the solid phase To enlarge the hydrogenation reaction process, the mass transfer efficiency between the respective reaction phases is increased and thereby the goal of enhancing the hydrogenation reaction at a given temperature and under a given pressure is achieved. Specifically, the hydrogen and the liquid and / or the solid-liquid mixture as the reaction raw material in the present exemplary embodiment are first fed into the micro-boundary generator before entering the fixed bed reactor 2 occur, through the microchannel effect or the mechanical effect in the microbubbles and / or microdroplets with a diameter of 1µm≤de <1mm in the micrometer range, and with other reaction phases form a microfluidic interface system, and finally enter the interior of the fixed bed reactor with the aid of a catalyst are fully reacted, and subsequently processed to form different reaction products. While using this system: the reaction pressure in the fixed bed reactor is 65% -80% of the internal pressure of the existing fixed bed reactor and the reaction temperature is 90% -94% of the existing reaction temperature, thereby drastically reducing the energy consumption and production cost during the reaction, reducing the capital investment , the service life of the plant is extended, poor intrinsic safety is ensured during the reaction, which effectively ensures the industrial mass production of the reaction products. It goes without saying that this reaction in the present embodiment is a type of reaction in which a fixed bed reactor is used for reaction enhancement so that the type of catalyst is not particularly limited, which is one or a combination of an iron-based catalyst, a Molybdenum-based catalyst, a nickel-based catalyst, a cobalt-based catalyst and a tungsten-based catalyst can act as long as it can be ensured that the amplification reaction proceeds smoothly.

With reference to the 5 there is further shown an emulsifying bed microinterfacial enhanced hydrogenation reaction system of an embodiment of the present utility model which has a reactor body 1 and a micro-interface generator 2 includes; being the reactor body 1 is an emulsification bed reactor that serves as a reaction chamber in the hydrogenation reaction to ensure that the hydrogenation reaction can sufficiently proceed; being a micro-boundary generator 2 is connected to the gas phase inlet and / or the liquid phase inlet on one side of the emulsification bed reactor, the number of which is provided two, one of which is arranged outside the emulsification bed reactor and the other is arranged inside the emulsification bed reactor, so that before the entry of hydrogen in the hydrogenation reaction process with a liquid and / or a solid-liquid mixture in the reactor body, the hydrogen and / or the liquid reactant in the micro-interface generator 2 using a predetermined process into which microbubbles and / or microdroplets in the micrometer range with a diameter of 1µm≤de <1mm are comminuted and form a microfluidic interface system with other reaction phases to form the phase boundary - mass transfer surface between the gas phase and / or the liquid phase and the liquid phase and / or to enlarge the solid phase in the hydrogenation reaction process, the mass transfer efficiency between the respective reaction phases being increased and thereby the aim of enhancing the hydrogenation reaction at a given temperature and under a given pressure is achieved. Specifically, the hydrogen and the liquid and / or the solid-liquid mixture as the reaction raw material in the present exemplary embodiment are first fed into the micro-interface generator before entering the emulsification bed reactor 2 occur through the mechanical action and the field force action in the microbubbles and / or microdroplets with a diameter in the micrometer range, and form a microfluidic interface system with other reaction phases, and finally enter the interior of the emulsifying bed reactor, are reacted with the aid of a catalyst, and then processed to form different reaction products. While using this system: the reaction pressure in the emulsifying bed reactor is 53% -76% of the internal pressure of the existing emulsifying bed reactor and the reaction temperature is 84% -89% of the existing reaction temperature, thereby drastically reducing the energy consumption and production cost during the reaction, reducing the investment strength , the service life of the plant is extended, poor intrinsic safety is ensured during the reaction, which effectively ensures the industrial mass production of the reaction products. It goes without saying that this reaction in the present embodiment is a kind of Is a reaction in which an emulsifying bed reactor is used for reaction enhancement so that the type of catalyst is not particularly limited, which is one or a combination of an iron-based catalyst, a molybdenum-based catalyst, a nickel-based catalyst, a cobalt-based catalyst and a tungsten-based catalyst as long as it can be ensured that the amplification reaction proceeds smoothly.

With reference to the 6th Also shown is a suspension bed microinterfacial enhanced hydrogenation reaction system of an embodiment of the present utility model which includes a reactor body 1 and a micro-interface generator 2 includes; being the reactor body 1 is a slurry bed reactor that serves as a reaction chamber in the hydrogenation reaction to ensure that the hydrogenation reaction can sufficiently proceed; where the micro-boundary generator 2 is connected to the gas phase inlet and / or liquid phase inlet at the lower end and the side part of the suspension bed reactor, so that before the entry of the hydrogen in the hydrogenation reaction process with a liquid and / or a solid-liquid mixture into the reactor body, the hydrogen and / or the liquid Reactant in the micro-interface generator using a predetermined process into the micro-bubbles and / or microdroplets in the micrometer range with a diameter of 1µm≤de <1mm are comminuted and form a microfluidic interface system with other reaction phases to form the phase boundary mass transfer surface between the gas phase and / or the liquid phase and to enlarge the liquid phase and / or the solid phase in the hydrogenation reaction process, the mass transfer efficiency between the respective reaction phases being increased and thereby the aim of enhancing the hydrogenation reaction at a given temperature and below r given pressure is reached. Specifically, the hydrogen and the liquid and / or the solid-liquid mixture as the raw material for the reaction in the present exemplary embodiment are first fed into the micro-interface generator before entering the suspension bed reactor 2 occur, crushed by the microchannel effect and the field force effect in the microbubbles and / or microdroplets with a diameter in the micrometer range, and form a microfluidic interface system with other reaction phases, and finally enter the interior of the suspension bed reactor, are reacted with the aid of a catalyst, and subsequently to Formation of different reaction products are processed. While using this system: the reaction pressure in the suspension bed reactor is 30% -48% of the internal pressure of the conventional suspension bed reactor (slurry bed reactor) and the reaction temperature is 78% -84% of the existing reaction temperature, which drastically reduces the energy consumption and the production cost during the reaction, the investment strength is reduced, the service life of the plant is extended, poor intrinsic safety is ensured during the reaction, which effectively ensures the industrial mass production of the reaction products. It goes without saying that this reaction in the present embodiment is a type of reaction in which a slurry bed reactor is used for reaction enhancement so that the type of catalyst is not particularly limited, which is one or a combination of an iron-based catalyst, a Molybdenum-based catalyst, a nickel-based catalyst, a cobalt-based catalyst and a tungsten-based catalyst can act as long as it can be ensured that the amplification reaction proceeds smoothly.

With reference to the 7th Also shown is a boiling bed microinterfacial enhanced hydrogenation reaction system of an embodiment of the present utility model which includes a reactor body 1 and a micro-interface generator 2 includes; being the reactor body 1 is a boiling bed reactor that serves as a reaction chamber in the hydrogenation reaction to ensure that the hydrogenation reaction can sufficiently proceed; where the micro-boundary generator 2 is connected to the gas phase inlet and / or liquid phase inlet at the lower end and the side part of the boiling bed reactor, so that before the entry of the hydrogen in the hydrogenation reaction process with a liquid and / or a solid-liquid mixture into the reactor body, the hydrogen and / or the liquid Reactant in the microinterfacial generator 2 using a predetermined process into which microbubbles and / or microdroplets in the micrometer range with a diameter of 1 µm≤de <1mm are comminuted and form a microfluidic interface system with other reaction phases to form the phase boundary mass transfer surface between the gas phase and / or the liquid phase and the liquid Phase and / or the solid phase in the hydrogenation reaction process to increase, the mass transfer efficiency between the respective reaction phases is increased and thereby the goal of enhancing the hydrogenation reaction at a given temperature and under a given pressure is achieved. Specifically, the hydrogen and the liquid and / or the solid-liquid mixture as the raw material for the reaction in the present exemplary embodiment are first introduced into the micro-interface generator before entering the boiling bed reactor 2 occur through the microchannel effect, the field force effect or the mechanical action in which microbubbles and / or microdroplets with a diameter in the micrometer range are crushed, and form a microfluidic interface system with other reaction phases, and finally enter the interior of the boiling bed reactor, are fully reacted with the aid of a catalyst, and are subsequently processed to form different reaction products. While using this system: the reaction pressure in the boiling bed reactor is 45% -78% of the internal pressure of the existing boiling bed reactor and the reaction temperature is 87% -93% of the existing reaction temperature, which drastically reduces the energy consumption and the production cost during the reaction, reducing the investment strength , the service life of the plant is extended, poor intrinsic safety is ensured during the reaction, which effectively ensures the industrial mass production of the reaction products. It goes without saying that this reaction in the present embodiment is a type of reaction in which a boiling bed reactor is used for reaction enhancement so that the type of the catalyst is not particularly limited, which is one or a combination of an iron-based catalyst, a Molybdenum-based catalyst, a nickel-based catalyst, a cobalt-based catalyst and a tungsten-based catalyst can act as long as it can be ensured that the amplification reaction proceeds smoothly.

Furthermore, the system according to the present utility model can be used in reactions of various types of oxidation reactions, chlorination reactions, carbonylation reactions and the breakdown of combustible ice, creating a micro-interface, a micro-nano-interface, an ultra-micro-interface, biochemical microbubble reactor or Microbubble bioreactor or the like device are formed, wherein an ultra-micro-mixing, a micro-fluidization, an ultra-micro-fluidization, a micro-bubble fermentation, a micro-bubble-bubble formation, a micro-bubble mass transfer, a micro-bubble transfer, a micro-bubble reaction, a micro-bubble absorption, a micro-bubble oxygenation, a micro-bubble contact or the like process or method is used to make the substances a multi-phase micro-mixing flow, a multi-phase micro-nano-flow, a multi-phase emulsification flow, a multi-phase microstructure flow, a gas Liquid-solid-micro-mixed flow, gas-liquid-solid-micro-nano-flow, a gas-liquid-solid-solid-emulsified flow, a gas-liquid-solid microstructure flow, a microbubble, a microbubble flow, a microfoam, a Micro-foam flow, a micro-gas-liquid flow, a gas-liquid-micro-nanoemulsion flow, an ultra-micro-flow, a micro-dispersion flow, a two-component micro-mixing flow, a microturbulence flow, a micro-bubble flow, a micro-bubble, a micro-bubble flow, a Form micro-nano-bubble and micro-nano-bubble flow and other micro-flow, thereby increasing the mass transfer area between the phases to increase the reaction efficiency between the phases.

It is obvious that in one of the present utility model provided micro-interface-enhanced hydrogenation reaction system, a micro-interface generator is connected to the reactor body, so that before the hydrogen enters the hydrogenation reaction process with a liquid and / or a solid-liquid mixture into the reactor body, the hydrogen and / or the liquid reactant in the micro-boundary surface generator is comminuted by means of a mechanical microstructure and / or a turbulent microstructure in a predetermined mode of action into the micro-bubbles and / or micro-droplets with a diameter in the micrometer range, so that the phase boundary-mass transfer surface between the hydrogen and the liquid and / or the solid-liquid mixture is effectively enlarged in the course of the reaction, as a result of which the mass transfer efficiency between the reaction phases is considerably improved, thus reinforcing the reaction ion is achieved in a given pressure range, while at the same time the energy consumption and the production costs are drastically reduced during the reaction, the investment strength is reduced, the service life of the plant is extended, a poor intrinsic safety is ensured during the reaction, which effectively increases the industrial mass production of the reaction products ensures.

In particular, in the micro-interface-enhanced hydrogenation reaction system that is provided by the present utility model, the selection of different types of comminution can be made according to the properties of the different reaction phases and the process requirements, such as the comminution of gases and / or liquids in the reaction medium through microchannels , Field or mechanical energy effect, which effectively ensures the effectiveness of the comminution of gases and / or liquids in a reaction medium before the entry of the reaction medium into the reactor body during the hydrogenation, whereby the phase boundary mass transfer efficiency in the gas phase, in the liquid phase and / or ensured between the gaseous phase, the liquid phase and the solid phase in the course of the reaction, whereby the reaction efficiency is further increased.

It is obvious that various modifications and variations can be made to the present utility model by those skilled in the art without departing from the spirit or scope of the present utility model. In this way, it is intended that the present utility model cover such modifications and variations, insofar as the changes and variations fall within the scope of the claims of the present utility model and their equivalent technologies.

Claims (10)

A microinterfacial enhanced hydrogenation reaction system characterized in that it comprises a reactor body serving as a reaction chamber in the hydrogenation reaction process to ensure that the hydrogenation reaction can sufficiently proceed; a micro-interface generator, which is connected to the reactor body, so that before the hydrogen enters the hydrogenation reaction process with a liquid and / or a solid-liquid mixture into the reactor body, the hydrogen and / or the liquid reactant in the micro-interface generator by means of a mechanical microstructure and / or a turbulent microstructure in a predetermined mode of action into which microbubbles and / or microdroplets with a diameter in the micrometer range are comminuted in order to increase the phase boundary mass transfer surface between the hydrogen and the liquid and / or solid-liquid mixture in the course of the reaction, wherein the mass transfer efficiency between the reaction phases is increased and the hydrogenation reaction rate is improved at a given temperature and under a given pressure. Microinterface-enhanced hydrogenation reaction system according to Claim 1 , characterized in that the predetermined mode of action is selected from one or more of the microchannel mode of action, the field force mode of action and the mechanical energy action; wherein the microchannel mode of action breaks up the gas phase and / or liquid phase passing through the microflow channel into the microbubbles and / or microdroplets by forming a microstructure of the flow channel; wherein the field force action by an external field force action supplies the energy into the liquid in a non-contact manner to break it up into the microbubbles or microdroplets; the mechanical energy action by the mechanical energy in the liquid converts it into a surface energy of the bubbles or droplets so that the bubbles or droplets are broken into the microbubbles or microdroplets. Microinterface-enhanced hydrogenation reaction system according to Claim 2 , characterized in that the microchannel mode of action is selected from one or more of a microporous ventilation process, a micronanoporous membrane process, a microflow channel process and a microfluidic process. Microinterface-enhanced hydrogenation reaction system according to Claim 2 , characterized in that the field force effect comprises a pressure field effect, a supergravity field effect, an ultrasonic field effect or an electromagnetic wave field effect. Microinterface-enhanced hydrogenation reaction system according to Claim 2 , characterized in that the mechanical energy application comprises an impingement flow fracture method, a vortex shear fracture method, a spray method, or a gas-liquid mixed flow pumping method. Micro-interface-enhanced hydrogenation reaction system according to one of the Claims 1 to 5 , characterized in that the reactor body comprises a tank reactor, a tubular reactor, a tower reactor, a fixed bed reactor or a fluidized bed reactor. Microinterface-enhanced hydrogenation reaction system according to Claim 6 , characterized in that the micro-boundary generator is connected to the gas phase and / or liquid phase inlet end of the reactor body, the number of which is provided as at least one group. Microinterface-enhanced hydrogenation reaction system according to Claim 1 , characterized in that the pre-set pressure range is between 10% and 80% of the pressure required for reactions in the existing reaction-enhancement systems. Microinterface-enhanced hydrogenation reaction system according to Claim 8 , characterized in that the area on the order of micrometers is greater than or equal to 1 µm and less than 1 mm. Micro-interface-enhanced hydrogenation reaction system according to one of the Claims 1 to 5 or 7th to 9 , characterized in that the micro-interface enhanced hydrogenation reaction system can be used in hydrogenation reactions in the fields of chemical industry, metallurgy, biotechnology, petroleum work, medicine, environmental treatment, biochemical fermentation, refineries, aquaculture, fine chemistry, biofermentation and mineral mining can.

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