JP3231870U - Micro-interface-enhanced hydrogenation reaction system - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a micro-interface-enhanced hydrogenation reaction system for increasing the phase boundary contact area of a reaction phase in the process of using the reaction-enhanced system. SOLUTION: In order to ensure that the hydrogenation reaction is sufficiently carried out, a reactor body 1 used as a reaction chamber in the process of the hydrogenation reaction and a mixed material of hydrogen and liquid and / or solid-liquid during the reaction process. Increases the interfacial material transfer area between the reaction phases, increases the efficiency of material transfer between the reaction phases, and under preset temperature and pressure conditions, the hydrogen and liquid and / or solid-liquid mixed material during the hydration reaction process enters the reactor. Before entering, hydrogen and / or liquid phase reactants are crushed into microbubbles and / or microdroplets of micron level in diameter by a preset method of action with mechanical microstructures and / or turbulent microstructures in a microinterface generator. The micro interface generator 2 is provided. [Selection diagram] Fig. 5

Description

This utility model relates to reaction strengthening technology, especially to a micro interface strengthening hydrogenation reaction system.

In fields such as energy, petrochemistry, and refining chemical industry, gas-liquid reaction processes such as gas-liquid and gas-liquid solid are widely present. For example, gas-liquid multiphase reactions such as oxidation, hydrogenation, and chlorination, and the macroreaction rate of these reactions are generally controlled by the mass transfer process. The mass transfer coefficient of a gas-liquid reaction is mainly influenced by the mass transfer coefficient and the gas-liquid phase boundary area. It is known that the influence of the phase boundary area on the volume mass transfer coefficient is relatively large and easy to control. Therefore, increasing the phase boundary area is regarded as an effective method for improving the gas-liquid macroreaction rate.

Bubbling Reactors and Stirring-Bubbling Reactors are currently commonly used gas-liquid reactors. Like the PX-oxidized TA tower bubbling reactor, the diameter of the bubbles is usually larger than 3 mm and can reach the cm class, so the mass transfer interface area is limited. In order to improve the macro reaction rate, it is necessary to promote liquid turbulence by increasing the amount of air blown, worsen the bursting of bubbles, increase the number of bubbles, and further increase the interface area. However, this inevitably reduces gas utilization, increases compressor power and exhaust gas emissions, and leads to excessive energy consumption, material loss and environmental pollution. Stirring-In the bubbling reactor, many large vortices that affect the micromotion of bubbles but have a small effect on bubble crushing are formed, and the bubbles cannot be crushed effectively, resulting in a large diameter and a limited mass transfer area. The reaction efficiency is lowered. In order to strengthen the gas-liquid mass transfer, it is common to add interiors such as a tower plate and a static mixer inside the tower of the tower type bubbling reactor to strengthen the mixing. Need to install structures such as stirring paddles or inner cylinders with different structures to increase the gas content of the liquid layer. The diameter of the bubbles obtained from these two types of reactors is usually 3-30 mm, and the supplied phase boundary area and mass transfer coefficient (liquid side, air side, solid liquid) are limited, so the reaction occurs. It will be difficult to obtain breakthrough improvements in performance.

Therefore, this practical proposal solves the problem that the existing hydrogenation reaction strengthening system increases the phase boundary area of each reaction phase by high temperature and high pressure in the process of reaction strengthening by providing a micro-interface strengthening hydrogenation reaction system. Is intended to be. Furthermore, it will bring challenges to large-scale industrialization due to high mass transfer speed, high energy consumption and production cost, strong investment intensity, short equipment operation cycle, frequent failures, poor intrinsic stability, etc. Solve.

This utility model is based on the reactor body used as a reaction chamber in the process of hydrogenation reaction to ensure that the hydrogenation reaction is sufficiently carried out.
Increases the interfacial material transfer area between hydrogen and liquid and / or solid-liquid mixed materials during the reaction process, increases the efficiency of material transfer between reaction phases, and the hydrogenation reaction rate of the reaction under preset temperature and pressure conditions. Connected to the reactor body and the hydrogen and / or the hydrogen and / or in the micro-interface generator before the liquid and / or solid-liquid mixture of hydrogen and liquid and / or solid-liquid mixture during the hydrogenation reaction process enters the reactor. With a Micro Interfacial Generator (MIG) that disrupts liquid phase reactants into microbubbles and / or microdroplets at the micron level in diameter with a preset method of action by mechanical microstructures and / or turbulent microstructures. To provide a micro-interface-enhanced hydrogenation reaction system comprising.

Further, in the micro-interface-enhanced hydrogenation reaction system, the preset action method is one or more selected from a microchannel action method, a force field action method and a mechanical energy action method; so,
In the microchannel action method, the gas phase and / or liquid phase passing through the microchannel is crushed into microbubbles and / or microdroplets by structuring the microstructure of the channel;
In the force field action method, energy is input to the fluid in a non-contact manner using an external force field, and the fluid is crushed into the microbubbles and / or microdroplets;
In the mechanical energy action method, the mechanical energy of a liquid is used to convert the surface energy of bubbles or droplets, and the bubbles or droplets are crushed into the microbubbles and / or microdroplets.

Further, in the micro-interface-enhanced hydrogenation reaction system, the micro-channel action method is one or a plurality of types selected from the micro-pore ventilation method, the micro-nanopore membrane method, the micro-channel method and the micro-channel control method. It is a thing.

Further, in the micro-interface-enhanced hydrogenation reaction system, the force field action method includes a pressure field action, a supergravity field action, an ultrasonic force field action, or a magnetic force field action.

Further, in the micro-interface-enhanced hydrogenation reaction system, the mechanical energy action method includes a collision flow crushing method, a swirling shear crushing method, a spray method or a gas-liquid mixed flow pump method.

Further, in the micro-interface-enhanced hydrogenation reaction system, the reactor body includes a kettle reactor, a tube reactor, a tower reactor, a fixed bed reactor or a fluidized bed reactor.

Further, in the micro-interface-enhanced hydrogenation reaction system, the micro-interface generator has at least one set of quantities and is connected to the gas phase and / or liquid phase inlet end of the reactor body.

Further, in the micro-interface-enhanced hydrogenation reaction system, the preset pressure range is 10% -80% of the pressure required for the reaction of the existing fortified reaction system.

Further, in the micro-interface-enhanced hydrogenation reaction system, the micron level range is 1 μm or more and less than 1 mm.

Further, in the micro-interface-enhanced hydrogenation reaction system, the micro-interference-enhanced hydrogenation reaction system includes chemical industry, metallurgy, biotechnology, petrochemical industry, pharmaceuticals, environmental management, biochemical fermentation, oil refining, aquatic culture, and precision chemistry. It can be used for hydrogenation reactions in the fields of industry, biological fermentation and mining of mineral products.

Compared with the existing technology, this utility model has the following beneficial effects: In the micro-interface-enhanced hydrogenation reaction system provided by this utility model, a micro-interface generator is provided in the reactor body. Mechanical microstructure and / or turbulence of the hydrogen and / or liquid phase reactant in a microinterface generator before the hydrogen and liquid and / or solid-liquid mixed material during the hydrogenation reaction enters the reactor body. Effective transfer area of interfacial material between hydrogen and liquid and / or solid-liquid mixed materials during the reaction process by crushing into microbubbles and / or microdroplets at the micron level in diameter by a method of action preset by the microstructure. The objectives of increasing the efficiency of transfer of material between the reaction phases and enhancing the hydrogenation reaction rate of the reaction under preset temperature and pressure conditions can be achieved, while at the same time energy consumption, production cost and The investment intensity can be significantly reduced, the equipment operation cycle can be extended, the intrinsic stability during the reaction process can be ensured, and the large-scale industrial production of the reaction product can be effectively guaranteed. Can be done.

In particular, in the micro-interface-enhanced hydrogenation reaction system provided by this utility model, different crushing methods can be selected according to the own characteristics of different reaction phases and the needs of the process. For example, by crushing a gas and / or liquid in the reaction medium by a microchannel, force field action or mechanical energy action, the reaction medium in the hydrogenation process is in the reaction medium before it enters the reactor body. Effectively ensures the effectiveness of crushing for gas and / or liquid, and at the same time guarantees the efficiency of phase substance transfer between the gas phase, liquid phase and / or gas phase, liquid phase and solid phase during the reaction process. Further, the reaction efficiency can be improved.

Other benefits and benefits of the Utility Model will become apparent by considering the following description of preferred embodiments made with reference to the accompanying drawings. It goes without saying that the accompanying drawings are merely for the purpose of exemplifying preferred embodiments, and the utility model is not limited to such embodiments. The same parts are indicated by the same reference symbols throughout the drawing.

It is a structural schematic diagram of the kettle type micro interface strengthening hydrogenation reaction system of one Embodiment of this utility model. It is a structural schematic diagram of the tube type micro interface strengthening hydrogenation reaction system of one Embodiment of this utility model. It is a structural schematic diagram of the tower type micro interface strengthening hydrogenation reaction system of one Embodiment of this utility model. It is a structural schematic diagram of the fixed layer micro interface strengthening hydrogenation reaction system of one Embodiment of this utility model. It is a structural schematic diagram of the emulsified layer micro interface strengthening hydrogenation reaction system of one Embodiment of this utility model. It is a structural schematic diagram of the floating layer micro interface strengthening hydrogenation reaction system of one Embodiment of this utility model. It is a structural schematic diagram of the boiling layer micro interface strengthening hydrogenation reaction system of one Embodiment of this utility model.

Hereinafter, embodiments of the utility model will be described in detail with reference to the accompanying drawings. It should be understood that the embodiments described below are exemplary and do not limit the utility model. Those skilled in the art are included in the scope of protection of the Utility Model, including other embodiments obtained from these embodiments without engaging in creative activities.

As shown in FIGS. 1 to 7, the micro-interface-enhanced hydrogenation reaction system according to the embodiment of the utility model includes a reactor body 1 and a micro-interface generator 2.

Here, the reactor body 1 is used as a reaction chamber in the process of the hydrogenation reaction to ensure that the hydrogenation reaction is sufficiently carried out; the micro-interface generator 2 is the reactor body. Connected to 1 and mechanically microstructured the hydrogen and / or liquid phase reactant with a micro-interface generator before the liquid and / or solid-liquid mixture of hydrogen and liquid and / or solid-liquid mixture during the hydrogenation reaction process enters the reactor. / Or crush into microbubbles and / or microdroplets at the micron level in diameter by the method of action preset by the turbulent microstructure, and form micro-interfaces, micro-nano-interfaces, ultra-fine interfaces, etc. in the reaction phase. Is for.

In addition, along with other reaction phases, polyphase micromixture, polyphase micronano flow, polyphase emulsification flow, polyphase microstructure flow, gas-liquid solid micromix flow, gas-liquid solid micro-nano flow, gas-liquid solid emulsification. Flow, gas-liquid solid microstructure flow, micro bubble, micro bubble flow, micro foam, micro foam flow, micro gas liquid flow, micro gas liquid nanoemulsion flow, ultrafine flow, microdisperse flow, biphasic micromixture, turbulence Polyphase fluid consisting of micro-sized particles such as flow, micro-bubble flow, micro-bubble, micro-bubble flow, micro-nano-bubble and micro-nano-bubble flow, or multi-phase fluid consisting of micro-sized particles (with micro-interfacial fluid) (Abbreviated) can be formed.

Furthermore, the mass transfer area between the gas phase and / or the liquid phase and the liquid phase and / or the solid phase during the hydrogenation reaction process is effectively increased, and the mass transfer efficiency between the hydrogen gas and each reaction phase is significantly increased. The purpose of improving and strengthening the hydrogenation reaction at relatively low preset temperature and pressure conditions is finally achieved, and at the same time, high temperature, high pressure, high consumption, high investment, high stability during the conventional hydrogenation reaction process. It is possible to effectively solve problems such as risks. As a result, the investment cost and operating cost of equipment can be significantly reduced.

In the present embodiment, hydrogen gas and other phase media as reaction raw materials first enter the micro-interface generator 2 before entering the reactor body 1, and the liquid and / or hydrogen during the hydrogenation reaction process. The gas is crushed into microbubbles and / or microdroplets at the micron level in diameter by microchannel action, force field action or mechanical energy action method through the internal mechanical microstructure and / or turbulent microstructure, and , Micro-interface, micro-nano-interface, ultra-fine interface, etc. can be formed.

In addition, when sufficiently mixed with other reaction phases, polyphase micromixture, polyphase micronano flow, polyphase emulsification flow, polyphase microstructure flow, gas-liquid solid micromix flow, gas-liquid solid micro-nano flow, gas-liquid Solid emulsification flow, gas-liquid solid microstructure flow, micro bubble, micro bubble flow, micro foam, micro foam flow, micro gas liquid flow, micro gas liquid nano emulsification flow, ultrafine flow, microdisperse flow, biphasic micromixture, Interfacial fluid reaction systems such as microturbulent flow, microbubble flow, microbubbles, microbubble flow, micronanobubbles and micronanobubble flow can be formed;

Finally, it can enter the inside of the reactor body 1 through the supply port of the reactor body 1 and react sufficiently with a catalyst to produce different reaction products through subsequent treatments. Furthermore, the mass transfer area between the gas phase and / or the liquid phase and the liquid phase and / or the solid phase during the hydrogenation reaction process is effectively increased, and the mass transfer efficiency between the hydrogen gas and each reaction phase is greatly improved. Finally, the purpose of strengthening the hydrogenation reaction within the pressure range of 10 to 80% of the pressure required for the reaction of the existing strengthening reaction system was realized. At the same time, problems such as high temperature, high pressure, high consumption, high investment, and high stability risk during the conventional hydrogenation reaction process can be effectively solved. As a result, the investment cost and operating cost of equipment can be significantly reduced.

Specifically, the reactor body 1 has a housing structure as a main place for reacting each reaction raw material in the hydrogenation reaction process. Specifically, by installing a kettle reactor, a tube reactor, a tower reactor, a fixed layer reactor and a fluidized bed reactor equipment, the hydrogenation reaction can be sufficiently carried out as a reaction chamber for a hydrogenation reaction. You just have to be able to react. Here, the fluidized bed reactor can be selected from any type of reactor such as an emulsion layer reactor, a floating layer reactor and a boiling layer reactor, depending on the reaction phase in the reaction raw material.

In the present embodiment, the specific type and structure of the reactor body 1 are different fields of use such as chemical industry, metallurgy, biotechnology, petrochemistry, pharmaceuticals, environment and biochemistry, and processes such as reaction temperature and reaction pressure. It can be selected or designed based on parameters such as parameters and quality requirements of the reaction product. If it can be ensured that the usage demand in the reaction process can be satisfied to the maximum, that is, the reaction speed and the quality of the finished product should be maximized, the cost input should be reduced, and the operation stability should be guaranteed. .. It should be understood that in different fields or different reaction processes, the specific structure of the reactor body 1 inevitably has some degree of discrimination, such as the location or quantity of supply ports.

Specifically, the micro interface generator 2 is provided at the gas phase and / or liquid inlet on the reactor body 1 as a core facility for crushing a gas and / or liquid in the hydrogenation reaction process, and the hydrogenation is performed. During the hydrogenation reaction process, the gas phase and / or liquid phase during the reaction process is subjected to a method such as microchannel action, force field action or mechanical energy action via the internal mechanical microstructure and / or turbulent microstructure. The mechanical energy of the gas and / or liquid phase is converted to the surface energy of the gas and / or liquid phase, and the gas and / or liquid phase is microbubbles and / or microbubbles with a diameter of 1 to 1000 μm. It can be crushed into microdroplets and form a microflow interface system with other reaction phases. As a result, the mass transfer area between the gas phase and / or the liquid phase and the liquid phase and / or the solid phase during the hydrogenation reaction process is effectively increased, and the mass transfer efficiency between the reaction phases is greatly improved. Finally, the purpose of enhancing the hydrogenation reaction at relatively low temperature and pressure conditions was achieved. At the same time, problems such as high temperature, high pressure, high consumption, high investment, and high stability risk during the conventional hydrogenation reaction process can be effectively solved. In addition, equipment investment and operating costs can be significantly reduced.

In the present embodiment, the micro interface generator 2 is connected in front of the supply port of the reactor body 1, and its specific position and quantity are the specific positions and quantities of the gas phase and / or liquid phase supply port of the reactor body 1. It can be determined by the position and quantity. For example, by being installed alone on the top, bottom or sides of the reactor, the corresponding top, bottom or side-mounted micro-interface-enhanced hydrogenation reaction systems can be formed and the top of the reactor. By being installed simultaneously on the bottom and sides, any number of horizontally opposed micro-interface-enhanced hydrogenation reaction systems can be formed. At the same time, the micro interface generator 2 is provided inside and / or outside the reactor body 1. In particular, the specific method by which the micro interface generator crushes the gas phase and / or the liquid phase during the hydrogenation reaction is a micro flow path action method or a force field action method according to a specific process demand. And one or more combinations can be selected from the mechanical energy action method.

Here, the microchannel action method crushes the gas phase and / or the liquid phase passing through the microchannel into microbubbles and / or microdroplets by structuring the microstructure of the channel. For example, micropore ventilation method, micronanopore membrane method (metal film, inorganic film or organic film, etc.), microchannel method or microchannel control method, etc .; Energy is input to the fluid by a non-contact method using an external field force such as a field, an ultrasonic force field, or a magnetic force field, and the fluid is crushed into the microbubbles or microdroplets; the mechanical energy action. The method uses the mechanical energy of the fluid to convert it to the surface energy of the bubbles or droplets, causing the bubbles or droplets to crush into the microbubbles or microdroplets. Here, the collision flow crushing method, the swirling shear crushing method, the spray method, the gas-liquid mixed flow pump method, and the like are included. Before the hydrogen gas and other reaction medium required for the reaction in the process of use enter the reactor body 1, the gas and / or liquid in the process of hydrogenation is first subjected to its internal microchannel, field action or It can be crushed into microbubbles and / or microdroplets having a diameter of 1 μm ≤ de <1 mm micron by a method such as mechanical energy action, and can form a micro interface, a micro nano interface, an ultrafine interface, and the like.

As a result, the phase-phase substance transfer area between the gas phase and / or the liquid phase and the liquid phase and / or the solid phase during the hydrogenation reaction process is effectively increased, and the substance transfer efficiency between each reaction phase during the reaction process is greatly increased. Finally achieved the purpose of strengthening the hydrogenation reaction within the pressure range of 10-80% of the pressure required for the reaction of the existing strengthening reaction system; at the same time, high temperature, high pressure, during the conventional hydrogenation reaction process. Problems such as high consumption, high investment, and high stability risk can be effectively solved, and the investment cost and operating cost of equipment can be significantly reduced.

Continuing with reference to FIG. 1, the micro-phase-enhanced hydrogenation reaction system of the embodiment of the present utility novel includes a reactor body 1 and a micro-phase generator 2; where the reactor body 1 is subjected to a hydrogenation reaction. A kettle reactor used as a reaction chamber in the course of the hydrogenation reaction to ensure that it is fully carried out; the micro interface generator 2 is the gas phase inlet and / or outer side of the kettle reactor. It is provided at the liquid phase inlet, and the number of installations is one, and the hydrogen and the liquid and / or solid-liquid mixed material during the hydrogenation reaction process enter the reactor before the hydrogen and the hydrogen and / or the solid-liquid mixed material enter the reactor. / Or by disrupting the liquid phase reactant into microbubbles and / or microdroplets at the micron level with a diameter of 1 μm ≤ de <1 mm in a preset manner and forming a microflow interface system with other reaction phases. , The purpose is to improve the phase-phase substance 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, and to increase the substance transfer efficiency between the reaction phases. Further, the purpose of enhancing the hydrogenation reaction under preset temperature and pressure conditions is realized.

In the present embodiment, the hydrogen gas and the liquid and / or solid-liquid mixed material as the reaction raw materials first enter the micro-interface generator 2 before entering the kettle reactor, and the microchannel method and the impact flow crushing method are performed. It is crushed into microbubbles and / or microdroplets at the micron level in diameter and forms a microflow interface system with other reaction phases, and finally enters the inside of the kettle reactor and reacts sufficiently with a catalyst. It is possible to produce different reaction products through subsequent processing. In the process of using this system, the reaction pressure inside the kettle reactor is 20% -50% of the existing internal pressure of the kettle reactor, and the reaction temperature is 87% -90% of the existing reaction temperature. Furthermore, the energy consumption, production cost and investment intensity in the reaction process can be significantly reduced, the equipment operation cycle can be extended, the intrinsic stability during the reaction process can be ensured, and the industrialization of the reaction product can be achieved. Large-scale production can be effectively guaranteed. Since this reaction in the present embodiment is one type of reaction in which the reaction is strengthened by a kettle reactor, the type of catalyst is not particularly limited, and iron-based catalyst, molybdenum-based catalyst, nickel-based catalyst, and cobalt are not particularly limited. It should be understood that one or a combination of one or more kinds of the system catalyst and the tungsten system catalyst may be used, and it is only necessary that the strengthening reaction can proceed smoothly.

Continuing with reference to FIG. 2, the tubular micro-phase-enhanced hydrogenation reaction system of the embodiment of the present utility novel includes a reactor body 1 and a micro-phase generator 2; where the reactor body 1 is hydrogenated. A tubular reactor used as a reaction chamber in the course of the hydrogenation reaction to ensure that the reaction is adequate; the micro interface generator 2 is the gas phase inlet at the outer apex of the tubular reactor and / Or provided both in front of the liquid phase inlet and inside the tubular reactor, the micro interface generator 2 before the hydrogen and liquid and / or solid-liquid mixture during the hydrogenation reaction enters the reactor 2 The hydrogen and / or liquid phase reactants are disrupted into microbubbles and / or microdroplets at the micron level with a diameter of 1 μm ≤ de <1 mm by a preset method, and the microflow interface system with other reaction phases. By forming the above, the phase-phase material 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 improved, and the material transfer efficiency between the reaction phases is increased. It is a thing. Further, the purpose of enhancing the hydrogenation reaction under preset temperature and pressure conditions is realized.

Specifically, in the present embodiment, the hydrogen gas and the liquid and / or solid-liquid mixed material as the reaction raw materials first enter the micro interface generator 2 before entering the tubular reactor, and the micro flow path method is performed. And by the impact flow crushing method, microbubbles and / or microdroplets with a diameter of micron level are crushed, and a microflow interface system is formed with other reaction phases, and finally, the inside of the tubular reactor is entered. It can react well with a catalyst and undergo subsequent treatments to produce different reaction products. In the process of using this system, the reaction pressure inside the tubular reactor is 30% -70% of the existing internal pressure of the tubular reactor, and the reaction temperature is 91% -94% of the existing reaction temperature. Furthermore, the energy consumption, production cost and investment intensity in the reaction process can be significantly reduced, the equipment operation cycle can be extended, the intrinsic stability during the reaction process can be ensured, and the industrialization of the reaction product can be achieved. Large-scale production can be effectively guaranteed. Since this reaction in the present embodiment is one type of reaction in which the reaction is strengthened by a tubular reactor, the type of catalyst is not particularly limited, and iron-based catalyst, molybdenum-based catalyst, nickel-based catalyst, and cobalt are not particularly limited. It should be understood that one or a combination of one or more kinds of the system catalyst and the tungsten system catalyst may be used, and it is only necessary that the strengthening reaction can proceed smoothly.

Continuing with reference to FIG. 3, the tower micro-phase-enhanced hydrogenation reaction system of the embodiment of the present utility includes a reactor body 1 and a micro-phase generator 2; where the reactor body 1 is hydrogenated. A tower reactor used as a reaction chamber in the course of the hydrogenation reaction to ensure that the reaction is adequate; the micro interface generator 2 is the gas phase inlet on the lower outer side of the tower reactor and The hydrogen and / or liquid phase is provided in front of the liquid phase inlet and is provided in the micro interface generator 2 before the hydrogen and liquid and / or solid-liquid mixed material during the hydrogenation reaction process enters the reactor. Hydrogenation reaction by disrupting the reactants into microbubbles and / or microdroplets at the micron level with a diameter of 1 μm ≤ de <1 mm in a preset manner and forming a microflow interface system with other reaction phases. The purpose is to improve the phase boundary substance transfer area between the gas phase and / or the liquid phase and the liquid phase and / or the solid phase in the process, and to increase the substance transfer efficiency between the reaction phases.

Further, the purpose of enhancing the hydrogenation reaction under preset temperature and pressure conditions is realized. Specifically, in the present embodiment, the hydrogen gas and the liquid and / or solid-liquid mixed material as the reaction raw materials first enter the micro-interface generator 2 before entering the tower reactor, and the micropore ventilation method is performed. , Microchannel method, Microchannel control method, Pressure field, Ultragravity field, Ultrasonic force field, Magnetic force field, Collision flow crushing method, Swirling shear crushing method, Spray method or Gas-liquid mixed flow It is crushed into microbubbles and / or microdroplets at the micron level in diameter by one or more pumping methods and forms a microflow interface system with other reaction phases, and finally, of the above-mentioned tower reactor. It can enter the interior and react sufficiently with the catalyst to produce different reaction products through subsequent treatments.

In the process of using this system, the reaction pressure inside the tower reactor is 10% -55% of the existing tower reactor internal pressure, and the reaction temperature is 87% -91% of the existing reaction temperature. Furthermore, the energy consumption, production cost and investment intensity in the reaction process can be significantly reduced, the equipment operation cycle can be extended, the intrinsic stability during the reaction process can be ensured, and the industrialization of the reaction product can be achieved. Large-scale production can be effectively guaranteed. Since this reaction in the present embodiment is one type of reaction in which the reaction is strengthened by a tower reactor, the type of catalyst is not particularly limited, and iron-based catalyst, molybdenum-based catalyst, nickel-based catalyst, and cobalt are not particularly limited. It should be understood that one or a combination of one or more kinds of the system catalyst and the tungsten system catalyst may be used, and it is only necessary that the strengthening reaction can proceed smoothly.

Continuing with reference to FIG. 4, the fixed-layer micro-phase-enhanced hydrogenation reaction system of the embodiment of the present utility novel includes a reactor body 1 and a micro-phase generator 2; where the reactor body 1 is hydrogenated. A fixed-layer reactor used as a reaction chamber in the course of the hydrogenation reaction to ensure that the reaction is adequate; the microinterface generator 2 is the gas phase on the outer top of the fixed-layer reactor. Provided in front of the inlet and / or liquid phase inlet and inside the fixed layer reactor, a micro interface is generated before the hydrogen and liquid and / or solid-liquid mixed material during the hydrogenation reaction process enters the reactor. By disrupting the hydrogen and / or liquid phase reactant in a vessel into micron-level microbubbles and / or microdroplets in a preset manner and forming a microflow interface system with other reaction phases. The purpose is to improve the phase-phase material 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, and to increase the material transfer efficiency between the reaction phases.

Further, the purpose of enhancing the hydrogenation reaction under preset temperature and pressure conditions is realized. Specifically, in the present embodiment, the hydrogen gas and the liquid and / or solid-liquid mixed material as the reaction raw materials first enter the micro-interface generator 2 and enter the microchannel before entering the fixed-layer reactor. By action or mechanical action, microbubbles and / or microdroplets having a diameter of 1 μm ≤ de <1 mm are crushed to form a microflow interface system with other reaction phases, and finally, the fixed layer type reaction. It can enter the interior of the vessel and react sufficiently with the catalyst to produce different reaction products through subsequent treatments. In the process of using this system, the reaction pressure inside the fixed layer reactor is 65% -80% of the existing internal pressure of the fixed layer reactor, and the reaction temperature is 90% -94% of the existing reaction temperature. Therefore, the energy consumption, production cost and investment intensity in the reaction process can be significantly reduced, the equipment operation cycle can be extended, the intrinsic stability during the reaction process can be ensured, and the reaction product. It is possible to effectively guarantee the large-scale production of industrialization.

Since this reaction in the present embodiment is a type of reaction in which the reaction is strengthened by a fixed layer reactor, the type of catalyst is not particularly limited, and iron-based catalysts, molybdenum-based catalysts, nickel-based catalysts, etc. It should be understood that one or a combination of one or more of the cobalt-based catalyst and the tungsten-based catalyst may be used, as long as the strengthening reaction can proceed smoothly.

Continuing with reference to FIG. 5, the emulsified layer micro-interface-enhanced hydrogenation reaction system of the embodiment of the present utility novel comprises a reactor body 1 and a micro-interface generator 2; where the reactor body 1 is hydrogenated. An emulsified layer reactor used as a reaction chamber in the course of the hydrogenation reaction to ensure that the reaction is adequate; the micro-interface generator 2 is the gas phase inlet on the side of the emulsified layer reactor and / Or installed in front of the liquid phase inlet, and the number of installations is two.

One is provided outside the emulsion layer reactor and the other is provided inside the emulsion layer reactor, and the hydrogen and liquid and / or solid-liquid mixed material during the hydrogenation reaction process is provided in the reactor. Prior to entry, the hydrogen and / or liquid phase reactant was disrupted into micron-level microbubbles and / or microdroplets with a diameter of 1 μm ≤ de <1 mm in the micro interface generator 2 by a preset method, and others. By forming a microflow interface system with the reaction phase of the above, the transfer area of the phase substance between the gas phase and / or the liquid phase and the liquid phase and / or the solid phase in the hydrogenation reaction process is improved, and between the reaction phases. This is to increase the efficiency of material transfer. Further, the purpose of enhancing the hydrogenation reaction under preset temperature and pressure conditions is realized.

Specifically, in the present embodiment, the hydrogen gas and the liquid and / or solid-liquid mixed material as the reaction raw materials first enter the micro-interface generator 2 before entering the emulsified layer reactor, and mechanically act and field. It is crushed into microbubbles and / or microdroplets at the micron level by force action, and forms a microflow interface system with other reaction phases, and finally enters the inside of the emulsified layer reactor and is sufficiently catalyst. And can produce different reaction products through subsequent processing. In the process of using this system, the reaction pressure inside the emulsion layer reactor is 53% -76% of the existing internal pressure of the emulsion layer reactor, and the reaction temperature is 84% -89% of the existing reaction temperature. Furthermore, the energy consumption, production cost and investment intensity in the reaction process can be significantly reduced, the equipment operation cycle can be extended, the intrinsic stability during the reaction process can be ensured, and the industrialization of the reaction product can be achieved. Large-scale production can be effectively guaranteed.

Since this reaction in the present embodiment is one type of reaction in which the reaction is strengthened in the emulsion layer reactor, the type of catalyst is not particularly limited, and iron-based catalyst, molybdenum-based catalyst, nickel-based catalyst, and cobalt are not particularly limited. It should be understood that one or a combination of one or more kinds of the system catalyst and the tungsten system catalyst may be used, and it is only necessary that the strengthening reaction can proceed smoothly.

Continuing with reference to FIG. 6, the floating layer micro-phase-enhanced hydrogenation reaction system of the embodiment of the present utility novel includes a reactor body 1 and a micro-phase generator 2; where the reactor body 1 is hydrogenated. A floating layer reactor used as a reaction chamber in the course of the hydrogenation reaction to ensure that the reaction is adequate; the micro-interface generator 2 is the bottom and side gas of the floating layer reactor. The hydrogen and / or liquid phase connected to the phase inlet and / or liquid phase inlet and at the micro interface generator before the hydrogen and liquid and / or solid-liquid mixed material during the hydrogenation reaction process enters the reactor. Hydrogenation reaction by disrupting the reactants into microbubbles and / or microdroplets at the micron level with a diameter of 1 μm ≤ de <1 mm in a preset manner and forming a microflow interface system with other reaction phases. The purpose is to improve the phase boundary substance transfer area between the gas phase and / or the liquid phase and the liquid phase and / or the solid phase in the process, and to increase the substance transfer efficiency between the reaction phases.

Further, the purpose of enhancing the hydrogenation reaction under preset temperature and pressure conditions is realized. Specifically, in the present embodiment, the hydrogen gas and the liquid and / or solid-liquid mixed material as the reaction raw materials first enter the micro-interface generator 2 before entering the floating layer reactor, and act as a microchannel. And by field action, it is crushed into microbubbles and / or microdroplets at the micron level in diameter, and forms a microflow interface system with other reaction phases, and finally enters the inside of the floating layer reactor and catalyzes. Can react more satisfactorily and produce different reaction products through subsequent processing. In the process of using this system, the reaction pressure inside the floating layer reactor is 30% -48% of the internal pressure of the existing floating layer reactor (paste layer), and the reaction temperature is 78% -84% of the existing reaction temperature. Since it is%, the energy consumption, production cost and investment intensity in the reaction process can be significantly reduced, the equipment operation cycle can be extended, and the intrinsic stability during the reaction process can be ensured. , It is possible to effectively guarantee the large-scale production of industrialization of reaction products.

Since this reaction in the present embodiment is one type of reaction in which the reaction is strengthened by the floating layer reactor, the type of catalyst is not particularly limited, and iron-based catalyst, molybdenum-based catalyst, nickel-based catalyst, and cobalt are not particularly limited. It should be understood that one or a combination of one or more kinds of the system catalyst and the tungsten system catalyst may be used, and it is only necessary that the strengthening reaction can proceed smoothly.

Continuing with reference to FIG. 7, the boiling layer micro-phase-enhanced hydrogenation reaction system of the embodiment of the present utility novel comprises a reactor body 1 and a micro-phase generator 2; where the reactor body 1 is hydrogenated. A boiling layer reactor used as a reaction chamber in the course of the hydrogenation reaction to ensure that the reaction is adequate; the micro-phase generator 2 is the bottom and side gas of the boiling layer reactor. Connected to the phase inlet and / or liquid phase inlet, the hydrogen and / or liquid in the micro interface generator 2 before the hydrogen and liquid and / or solid-liquid mixed material during the hydrogenation reaction process enters the reactor. Hydrogenation by disrupting the phase reactants into micron-level microbubbles and / or microdroplets with a diameter of 1 μm ≤ de <1 mm in a preset manner and forming a microflow interface system with other reaction phases. The purpose is to improve the phase boundary substance transfer area between the gas phase and / or the liquid phase and the liquid phase and / or the solid phase in the reaction process, and to increase the substance transfer efficiency between the reaction phases. Further, the purpose of enhancing the hydrogenation reaction under preset temperature and pressure conditions is realized.

Specifically, in the present embodiment, the hydrogen gas and the liquid and / or solid-liquid mixed material as the reaction raw materials first enter the micro-interface generator 2 before entering the boiling layer reactor, and act as a microchannel. It is crushed into microbubbles and / or microdroplets at the micron level in diameter by field force or mechanical action, and forms a microflow interface system with other reaction phases, and finally inside the floating layer reactor. It can enter and react well with the catalyst to produce different reaction products through subsequent treatments. In the process of using this system, the reaction pressure inside the boiling layer reactor is 45% -78% of the existing internal pressure of the boiling layer reactor, and the reaction temperature is 87% -93% of the existing reaction temperature. Furthermore, the energy consumption, production cost and investment intensity in the reaction process can be significantly reduced, the equipment operation cycle can be extended, the intrinsic stability during the reaction process can be ensured, and the industrialization of the reaction product can be achieved. Large-scale production can be effectively guaranteed.

Since this reaction in the present embodiment is a type of reaction in which the reaction is strengthened by a boiling layer reactor, the type of catalyst is not particularly limited, and iron-based catalyst, molybdenum-based catalyst, nickel-based catalyst, and cobalt are not particularly limited. It should be understood that one or a combination of one or more kinds of the system catalyst and the tungsten system catalyst may be used, and it is only necessary that the strengthening reaction can proceed smoothly.

Furthermore, the system of the present practical novel can be used for reaction processes such as various types of oxidation reactions, chlorination reactions, carbonylation reactions and flammable ice mining, and further micro-interfaces, micro-nano-interfaces, and ultra-fine interfaces. , Microbubble bioreactors or microbubble bioreactors can be formed. Processes or methods such as micro-mixing, micro-flowing, ultra-micro-flowing, micro-bubble fermentation, micro-bubble bubbles, micro-bubble material transfer, micro-bubble transmission, micro-bubble reaction, micro-bubble absorption, micro-bubble oxygen increase, micro-bubble contact, etc. Depending on the material, polyphase micromix flow, polyphase micronano flow, polyphase emulsification flow, polyphase microstructure flow, gas-liquid solid micromix flow, gas-liquid solid micro-nano flow, gas-liquid solid emulsification flow, gas-liquid solid micro Structural flow, microbubbles, microbubble flow, microbubbles, microbubble flow, microgas-liquid flow, gas-liquid micro-nano-emulsified flow, ultrafine flow, microdispersed flow, biterm micromixed flow, microturbulent flow, microbubble flow, It is possible to form microfluids such as microbubbles, microbubble flow, micronanobubbles, and micronanobubble flow. Therefore, the mass transfer area between the phases is increased to improve the reaction efficiency between the phases.

As is clear from the above description, in the micro-interface-enhanced hydrogenation reaction system provided by the present practical novel, a micro-phase-enhanced generator is provided in the reactor body, and hydrogen and liquid and / or solid during the hydrogenation reaction process. Before the liquid mixture material enters the reactor body, the hydrogen and / or liquid phase reactant is subjected to the micro-microstructure at the micron level in diameter by the mechanism of action preset by the mechanical microstructure and / or the turbulent flow microstructure in the micro interface generator. By crushing into bubbles and / or microdroplets, the transfer area of the phase substance between hydrogen and the liquid and / or solid-liquid mixed material during the reaction process is effectively increased, and the efficiency of substance transfer between the reaction phases is extremely enhanced. Achieves the purpose of enhancing the hydrogenation reaction rate of the reaction under preset temperature and pressure conditions, while simultaneously significantly reducing energy consumption, production cost and investment intensity, extending the equipment operation cycle. Therefore, the intrinsic stability during the reaction process can be ensured, and the large-scale industrial production of the reaction product can be effectively guaranteed.

In particular, in the micro-interface-enhanced hydrogenation reaction system provided by this utility model, different crushing methods can be selected according to the own characteristics of different reaction phases and the needs of the process. For example, by crushing a gas and / or liquid in the reaction medium by a microchannel, force field action or mechanical energy action, the reaction medium in the hydrogenation process is in the reaction medium before it enters the reactor body. Effectively ensures the effectiveness of crushing for gas and / or liquid, and at the same time guarantees the efficiency of phase substance transfer between the gas phase, liquid phase and / or gas phase, liquid phase and solid phase during the reaction process. Further, the reaction efficiency can be improved.

It is clear that those skilled in the art can make various changes and modifications that do not deviate from the spirit and purpose of this utility model. As such, the described embodiments are intended to include the spirit of the utility model claims and all such modifications and modifications within the scope of the utility model registration claims.

Claims (10)

To ensure that the hydrogenation reaction is sufficiently carried out, the reactor body used as a reaction chamber in the process of the hydrogenation reaction and the boundary material between the hydrogen and the liquid and / or solid-liquid mixed material during the reaction process. The hydrogenation is connected to the reactor body to increase the transfer area, increase the efficiency of transfer of material between the reaction phases, and enhance the hydrogenation reaction rate of the hydrogenation reaction under preset temperature and pressure conditions. The hydrogen and / or liquid phase reactant is preset by mechanical microstructure and / or turbulent microstructure in a micro interface generator before the hydrogen and liquid and / or solid-liquid mixture during the reaction process enters the reactor. A micro-interface-enhanced hydrogenation reaction system comprising a micro-interface generator that crushes into micro-bubbles and / or micro-droplets of micron level in the manner of action. The preset action method is selected from a microchannel action method, a force field action method, and a mechanical energy action method, and is one or more types.
In the microchannel action method, the gas phase and / or liquid phase passing through the microchannel is crushed into microbubbles and / or microdroplets by constructing the microstructure of the channel.
In the force field action method, energy is input to the fluid in a non-contact manner using an external force field, and the fluid is crushed into the microbubbles and / or microdroplets.
The mechanical energy action method is characterized in that the mechanical energy of a fluid is used to convert the surface energy of bubbles or droplets, and the bubbles or droplets are crushed into the microbubbles and / or microdroplets. The micro-interface-enhanced hydrogenation reaction system according to claim 1. 2. The method according to claim 2, wherein the microchannel action method is one or a plurality of types selected from a micropore ventilation method, a micronanopore membrane method, a microchannel method, and a microchannel control method. The micro-interface-enhanced hydrogenation reaction system described. The micro interface-enhanced hydrogenation reaction according to claim 2, wherein the force field action method includes a pressure field action, a supergravity field action, an ultrasonic force field action, or a magnetic force field action. system. The micro-interface-enhanced hydrogenation reaction system according to claim 2, wherein the mechanical energy action method includes a collision flow crushing method, a swirling shear crushing method, a spray method, or a gas-liquid mixed flow pump method. The invention according to any one of claims 1 to 5, wherein the reactor body includes a kettle reactor, a tube reactor, a tower reactor, a fixed bed reactor or a fluidized bed reactor. Micro interface strengthening hydrogenation reaction system. The micro-interface-enhanced hydrogenation according to claim 6, wherein the micro-interface generator has at least one set quantity and is connected to the gas phase and / or liquid phase inlet end of the reactor body. Reaction system. The micro-interface-enhanced hydrogenation reaction system according to claim 2, wherein the preset pressure range is 10% to 80% of the pressure required for the reaction of the existing intensification reaction system. The micro-interface-enhanced hydrogenation reaction system according to claim 8, wherein the micron level range is 1 μm or more and less than 1 mm. The micro-interface-enhanced hydrogenation reaction system is used for hydrogenation in the fields of chemical industry, metallurgy, biotechnology, petrochemical industry, pharmaceuticals, environmental management, biochemical fermentation, oil refining, aquatic cultivation, precision chemical industry, biological fermentation and mineral product mining. The micro-interface-enhanced hydrogenation reaction system according to any one of claims 1 to 5 or 7 to 9, wherein it can be used in a reaction.

Images