WO2020186634A1

WO2020186634A1 - Micro-interface enhanced hydrogenation reaction system

Info

Publication number: WO2020186634A1
Application number: PCT/CN2019/090268
Authority: WO
Inventors: 张志炳; 周政; 张锋; 李磊; 孟为民; 王宝荣; 杨高东; 罗华勋; 杨国强; 田洪舟
Original assignee: 南京延长反应技术研究院有限公司
Priority date: 2019-03-15
Filing date: 2019-06-06
Publication date: 2020-09-24
Also published as: DE212019000177U8; CN111359556A; JP3231870U; DE212019000177U1; RU207190U1; AU2019101747A4

Abstract

A micro-interface enhanced hydrogenation reaction system, comprising: a reactor main body (1), used as a reaction chamber during a hydrogenation reaction process; a micro-interface generator (2), connected to the reactor main body (1) and used for crushing hydrogen gas and/or liquid reactants into micro-bubbles and/or micro-droplets having micrometer-level diameters by means of a mechanical microstructure and/or turbulent microstructure in the micro-interface generator (2) using a preset action mode before hydrogen gas, liquid and/or solid-liquid mixture materials enter the reactor main body (1) during the hydrogenation reaction process, thereby increasing the phase-boundary mass transfer area between the hydrogen gas, liquid and/or solid-liquid mixture materials in the reaction process, improving the mass transfer efficiency between reaction phases, and strengthening the hydrogenation reaction under preset temperature and pressure conditions.

Description

Micro-interface strengthening hydrogenation reaction system

Technical field

The invention belongs to the technical field of reaction strengthening, and specifically relates to a micro-interface strengthening hydrogenation reaction system.

Background technique

Gas-liquid, gas-liquid-solid and other gas-liquid reaction processes are widely present in the fields of energy, petrochemical, and fine chemicals. For gas-liquid multiphase reactions such as oxidation, hydrogenation, and chlorination, the macroscopic reaction rate is generally restricted by the mass transfer process. The volumetric mass transfer coefficient of the gas-liquid reaction is mainly affected by the mass transfer coefficient and the area of the gas-liquid phase boundary. Studies have shown that the phase boundary area has a greater influence on the volumetric mass transfer coefficient and is easy to control. Therefore, increasing the phase boundary area is regarded as an effective way to increase the gas-liquid macroscopic reaction rate.

Bubbling reactors and stirred-bubbling reactors are currently commonly used gas-liquid reactors. For example, in the tower bubbling reactor of PX oxidation to TA, the bubble diameter is usually larger than 3mm, or even centimeter level, and its mass transfer interface area is limited. In order to increase the macroscopic reaction rate, the turbulence of the liquid must be promoted by increasing the amount of air blown, so that the bursting of the bubbles is intensified to increase the number of bubbles, and thus the interface area. This will inevitably reduce the gas utilization rate, increase the compressor power and exhaust emissions, and cause the transition of energy consumption, material loss and environmental pollution. Stirring-bubbling gas-liquid reactors often form large vortices that affect the macroscopic movement of bubbles but have little effect on bubble breaking. The bubbles cannot be broken effectively, so the diameter is too large and the mass transfer area is limited, resulting in low reaction efficiency. . In order to strengthen gas-liquid mass transfer, tower bubbling reactors generally add trays, static mixers and other internals in the tower to enhance mixing, while stirring tanks need to install different structures of stirring blades or inner cylinders to increase The gas content of the liquid layer. In these two reactors, the bubble diameter is usually 3-30mm, and the phase boundary area and mass transfer coefficient (liquid side, gas side, solid-liquid) provided are limited, so it is difficult to achieve breakthrough improvement in reaction performance.

Summary of the invention

In view of this, the present invention proposes a micro-interface strengthening hydrogenation reaction system, which aims to solve the problem of increasing the phase boundary area of each reaction phase by means of high temperature and high pressure in the existing hydrogenation reaction strengthening system during the reaction strengthening process. Furthermore, while increasing the mass transfer rate, it is easy to cause problems such as high energy consumption and production cost, high investment intensity, short equipment operation cycle, multiple failures, and poor intrinsic safety, which pose challenges to industrial mass production.

The present invention provides a micro-interface strengthening hydrogenation reaction system, which includes:

The main body of the reactor is used as a reaction chamber in the hydrogenation reaction process to ensure that the hydrogenation reaction can fully proceed;

Micro Interfacial Generator (MIG), which is connected to the main body of the reactor, and is used for the hydrogen and liquid and/or solid-liquid mixture in the hydrogenation process to enter the main body of the reactor. Previously, the hydrogen and/or liquid phase reactant was broken into micro bubbles and/or micro droplets with a diameter of micrometers in a predetermined action mode through mechanical microstructures and/or turbulent microstructures in the micro-interface generator , In order to increase the mass transfer area of the phase boundary between the hydrogen and the liquid and/or solid-liquid mixture during the reaction, improve the mass transfer efficiency between the reaction phases, and strengthen the mass transfer under the preset temperature and pressure conditions. The reaction rate of hydrogenation.

Further, in the aforementioned micro-interface strengthening hydrogenation reaction system, the preset mode of action is selected from one or more of the mode of microchannel action, the action of field force, and the action of mechanical energy; wherein,

The microchannel action mode is to construct the microstructure of the flow channel, so that the gas and/or liquid phase passing through the micro flow channel is broken into micro bubbles and/or micro droplets;

The field force action mode is to use external field force to input energy into the fluid in a non-contact manner to break it into the microbubbles or microdroplets;

The action mode of the mechanical energy is to use the mechanical energy of the fluid to convert it into the surface energy of bubbles or droplets, so that the bubbles or droplets are broken into the microbubbles or microdroplets.

Further, in the aforementioned micro-interface strengthening hydrogenation reaction system, the micro-channel action mode is selected from one or more of micro-porous aeration method, micro-nano-porous membrane method, micro-channel method and micro-fluidic method.

Further, in the micro-interface strengthening hydrogenation reaction system, the field force action mode includes: pressure field action, supergravity field action, ultrasonic field action or electromagnetic wave field action.

Further, in the above-mentioned micro-interface strengthening hydrogenation reaction system, the action mode of the mechanical energy includes: impinging stream breaking method, cyclotron shear breaking method, spray method or gas-liquid mixed flow pump method.

Further, in the aforementioned micro-interface strengthening hydrogenation reaction system, the reactor main body includes: a tank reactor, a tubular reactor, a tower reactor, a fixed bed reactor or a fluidized bed reactor.

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

Further, in the aforementioned micro-interface intensified hydrogenation reaction system, the preset pressure range is 10%-80% of the pressure required by the existing hydrogenation intensified reaction system.

Further, in the aforementioned micro-interface strengthening hydrogenation reaction system, the range of the micron level is greater than or equal to 1 μm and less than 1 mm.

Further, in the above-mentioned micro-interface intensified hydrogenation reaction system, the micro-interface intensified hydrogenation reaction system can be applied to chemical industry, metallurgy, bioengineering, petrochemical industry, medicine, environmental treatment, biochemical fermentation, oil refining, aquaculture, fine chemical industry , Biological fermentation and hydrogenation reactions in the field of mineral mining.

Compared with the prior art, the beneficial effect of the present invention is that the micro-interface strengthening hydrogenation reaction system provided by the present invention, by connecting the micro-interface generator to the main body of the reactor, the hydrogen and liquid in the hydrogenation reaction process And/or the solid-liquid mixture material breaks the hydrogen and/or liquid phase reactants in the micro-interface generator through mechanical microstructures and/or turbulent microstructures in a predetermined action mode before entering the reactor body Micro-bubbles and/or micro-liquid droplets with a diameter of micrometers are formed, which effectively increases the mass transfer area of the phase boundary between the hydrogen and the liquid and/or solid-liquid mixture during the reaction process, and greatly improves the interaction between the reaction phases. The mass transfer efficiency achieves the purpose of strengthening the reaction within the lower preset pressure range, while greatly reducing the energy consumption and production cost in the reaction process, reducing the investment intensity, extending the equipment operation cycle, and ensuring the reaction The intrinsic safety of the process is poor, which effectively guarantees the industrialized mass production of reaction products.

In particular, in the micro-interface strengthening hydrogenation reaction system provided by the present invention, different crushing methods can be selected according to the characteristics of different reaction phases and process requirements, such as microchannels, field forces or mechanical energy effects on the reaction medium. The gas and/or liquid crushing effectively ensures the effectiveness of crushing the gas and/or liquid in the reaction medium before the reaction medium enters the main body of the reactor during the hydrogenation process, and ensures the gas, liquid and/or liquid phase and/or The mass transfer efficiency between the gas phase, the liquid phase and the solid phase further improves the reaction efficiency.

Description of the drawings

By reading the detailed description of the preferred embodiments below, various other advantages and benefits will become clear to those of ordinary skill in the art. The drawings are only used for the purpose of illustrating the preferred embodiments, and are not considered as a limitation to the present invention. Also, throughout the drawings, the same reference symbols are used to denote the same components. In the attached picture:

Figure 1 is a schematic structural diagram of a kettle-type micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention;

2 is a schematic structural diagram of a tubular micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention;

Figure 3 is a schematic structural diagram of a tower-type micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention;

4 is a schematic structural diagram of a fixed bed micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention;

5 is a schematic structural diagram of an emulsion bed micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention;

6 is a schematic structural diagram of a suspended bed micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention;

Fig. 7 is a schematic structural diagram of a fluidized bed micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention.

detailed description

The technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative work shall fall within the protection scope of the present invention.

Referring to Figures 1-7, the micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention includes: a reactor body 1 and a micro-interface generator (MIG) 2; wherein, the reactor body 1 is used for hydrogenation The reaction chamber during the reaction process to ensure that the hydrogenation reaction can fully proceed; the micro-interface generator 2 is connected to the reactor main body 1 for the hydrogen and liquid and/or liquid and/or Before the solid-liquid mixture material enters the reactor body, the hydrogen and/or liquid phase reactants are broken into diameters in the micro-interface generator through mechanical microstructures and/or turbulent microstructures in a preset mode of action. Micron-level micro bubbles and/or micro-droplets to form micro-interfaces, micro-nano interfaces, ultra-micro interfaces, etc. in other reaction phases, and together with other reaction phases to form multi-phase micro-mixed flow, multi-phase micro-nano flow, Multiphase emulsified flow, multiphase microstructure flow, gas-liquid-solid micro-mixed flow, gas-liquid-solid micro-nano flow, gas-liquid-solid emulsified flow, gas-liquid-solid microstructure flow, microbubble, microbubble flow, microbubble, microbubble flow , Micro-gas-liquid flow, gas-liquid micro-nano emulsified flow, ultra-micro flow, micro-dispersion flow, two-phase micro-mixed flow, micro-turbulent flow, micro bubble flow, micro bubble, micro bubble flow, micro nano bubble and micro nano bubble Bubble flow and other multiphase fluids formed by micro-scale particles, or multi-phase fluids formed by micro-nano-scale particles (referred to as micro-interface fluids), thereby effectively increasing the gas and/or liquid phases during the hydrogenation reaction. The mass transfer area of the phase boundary between the phase and the liquid phase and/or the solid phase greatly improves the mass transfer efficiency between the hydrogen and the reaction phases, and finally realizes the strengthening of the mass transfer area under the lower preset temperature and pressure conditions. The purpose of the hydrogenation reaction is to effectively solve the problems of high temperature, high pressure, high material consumption, high investment, high safety risk, etc. in the traditional hydrogenation reaction process, thereby significantly reducing equipment investment costs and operating costs.

In this embodiment, the hydrogen and other phase media as the reaction raw materials enter the micro-interface generator 2 before entering the reactor body 1, and the mechanical microstructure and/or turbulent microstructure inside it Microchannel action, field force action or mechanical energy action breaks the liquid and/or hydrogen during the hydrogenation reaction process into microbubbles and/or microdroplets with a diameter on the order of microns to form microinterfaces, micronanointerfaces or Ultra-micro interface, etc.; then fully mixed with other reaction phases to form multi-phase micro-mixed flow, multi-phase micro-nano flow, multi-phase emulsification flow, multi-phase micro-structure flow, gas-liquid-solid micro-mixed flow, gas-liquid-solid micro-nano flow, Gas-liquid-solid emulsified flow, gas-liquid-solid microstructure flow, microbubble, microbubble flow, microfoam, microfoam flow, microgas liquid flow, gas-liquid micro-nano emulsion flow, ultra micro flow, micro dispersion flow, two micro Micro-interface fluid reaction systems such as mixed flow, micro-turbulent flow, micro-bubble flow, micro-bubble, micro-bubble flow, micro-nano bubbling and micro-nano bubbling flow; finally enter the reactor through the feed port of the reactor body 1 The inside of the reactor body 1 fully reacts under the action of the catalyst, and undergoes subsequent treatment to form different reaction products, thereby effectively increasing the hydrogen and/or liquid phase and the liquid and/or solid phase in the reaction process. The mass transfer area of the phase boundary further improves the mass transfer efficiency between hydrogen and each reaction phase during the hydrogenation reaction, and finally achieves the intensified heating within the range of 10%-80% of the pressure required by the existing intensified reaction system. The purpose of the hydrogen reaction: At the same time, it effectively solves the problems of high temperature, high pressure, high material consumption, high investment, high safety risk, etc. in the traditional hydrogenation process, thereby significantly reducing equipment investment costs and operating costs.

Specifically, the reactor main body 1 serves as the main place where each reaction raw material reacts during the hydrogenation reaction, and the whole is a shell structure, which can specifically be: a tank reactor, a tubular reactor, a tower The reactor, the fixed bed reactor and the fluidized bed reactor, as long as it can be used as the reaction chamber of the hydrogenation reaction, to ensure that the hydrogenation reaction can fully react, and the fluidized bed reactor can be based on the reaction raw materials. Different reaction phases can be selected from any type of reactor such as emulsified bed reactor, suspended bed reactor, and fluidized bed reactor.

In this embodiment, the specific type and structure of the reactor body 1 may be based on different application fields such as chemical industry, metallurgy, bioengineering, petrochemical industry, medicine, environment, and biochemistry, process parameters such as reaction temperature and reaction pressure, and reaction products. Quality requirements and other parameters are selected or designed, as long as it can ensure that the use requirements can be met to the greatest extent during the reaction process, that is, to maximize the reaction rate, improve the quality of the finished product, reduce cost input and ensure safe operation. It is understandable that the specific structure of the reactor main body 1 in different fields or different reaction processes inevitably has a certain degree of difference, for example, the positions and numbers of the inlet and outlet ports are not the same.

Specifically, the micro-interface generator 2 is used as the core equipment for crushing gas and/or liquid in the hydrogenation reaction process. It is provided with a gas and/or liquid feed port on the reactor body 1, and the The gas and/or liquid phase in the hydrogenation reaction process converts the mechanical energy of the gas and/or liquid phase through the mechanical microstructure and/or turbulent microstructure through microchannel action, field force action or mechanical energy action, etc. The surface energy of the gas phase and/or liquid phase, which breaks the gas phase and/or liquid phase into micro-scale micro-bubbles and/or micro-droplets with a diameter of 1-1000 μm, and forms a micro-flow interface with other reaction phases System, thereby effectively increasing the mass transfer area of the phase boundary between the gas and/or liquid phase and the liquid and/or solid phase during the hydrogenation reaction process, greatly improving the mass transfer between the reaction phases Efficiency, finally achieves the purpose of strengthening the hydrogenation reaction under lower temperature and pressure conditions, and at the same time effectively solves the problems of high temperature, high pressure, high material consumption, high investment, and high safety risks in the traditional hydrogenation process. This significantly reduces equipment investment costs and operating costs.

In this embodiment, the micro-interface generator 2 is connected in front of the feed port of the reactor main body 1, and its specific position and number can be based on the specific position of the gas and/or liquid phase feed port on the reactor main body 1. It can be set separately at the top, bottom or side of the reactor to form corresponding top-mounted, bottom-mounted and side-mounted micro-interface intensified hydrogenation reaction systems. It can also be installed at the top of the reactor at the same time. The bottom and sides are used to form a variety of opposing micro-interface strengthening hydrogenation reaction systems. At the same time, the micro-interface generator 2 is arranged inside and/or outside the reactor body 1. In particular, the specific method for the micro-interface generator to break the gas phase and/or the liquid phase in the hydrogenation reaction can also be selected according to specific process requirements. One of the microchannel action mode, field force action mode, and mechanical energy action mode can also be selected. One or several combinations; wherein, the micro-channel action mode is by constructing the micro-structure of the flow channel, so that the gas and/or liquid phase passing through the micro-channel is broken into micro bubbles and/or micro droplets, such as micropores Aeration method, micro-nanoporous membrane method (various metal membranes, inorganic membranes or organic membranes), micro-channel method or micro-fluidic method, etc.; the field force action method is the use of pressure field, high gravity field, ultrasonic field or The electromagnetic wave field and other external field forces input energy into the fluid in a non-contact manner, causing it to break into the microbubbles or microdroplets; the mechanical energy action method is to use the mechanical energy of the fluid to convert it into bubbles or droplets on the surface Yes, the bubbles or droplets can be broken into the microbubbles or microdroplets, which include: impinging stream breaking method, whirling shear breaking method, spray method, gas-liquid mixed flow pump method, etc. In the process of use, the hydrogen and other reaction media required for the reaction enter the reactor body 1 before entering the reactor body 1 through microchannels, field forces, or mechanical energy. / Or the liquid is broken into micron-level micro-bubbles and/or micro-droplets with a diameter of 1μm≤de<1mm to form micro-interface, micro-nano interface or ultra-micro interface, etc., effectively increasing the hydrogenation reaction The mass transfer area of the phase boundary between the gas and/or liquid phase and the liquid and/or solid phase in the process, thereby improving the mass transfer efficiency between the reaction phases in the reaction process, and finally achieving the reaction in the existing enhanced reaction system The purpose of strengthening the hydrogenation reaction within the pressure range of 10%-80% of the required pressure; at the same time, it effectively solves the problems of high temperature, high pressure, high material consumption, high investment, and high safety risk in the traditional hydrogenation reaction process, thereby significantly reducing Equipment investment costs and operating expenses.

Continuing to refer to Figure 1, it is a micro-interface strengthening hydrogenation reaction system of an embodiment of the present invention, which includes: a reactor main body 1 and a micro-interface generator 2; wherein the reactor main body 1 is a tank reactor for The reaction chamber for the hydrogenation reaction to ensure that the hydrogenation reaction can be fully carried out; the micro-interface generator 2 is connected to the gas-phase inlet and/or the liquid-phase inlet on the outer side of the tank reactor, and the set number is one, The hydrogen and liquid and/or solid-liquid mixture materials used in the hydrogenation reaction process pass the hydrogen and/or liquid phase reactants through the micro-interface generator before entering the reactor body. Suppose the method is broken into micro-sized bubbles and/or micro-droplets with a diameter of 1μm≤de<1mm, and forms a microfluidic interface system with other reaction phases to increase the gas and/or liquid phases during the hydrogenation reaction. The mass transfer area of the phase boundary between the phase and the liquid phase and/or the solid phase improves the mass transfer efficiency between the reaction phases, and achieves the purpose of strengthening the hydrogenation reaction under preset temperature and pressure conditions. In this embodiment, the hydrogen and liquid and/or solid-liquid mixtures as raw materials for the reaction enter the micro-interface generator 2 before entering the tank reactor and are crushed by the micro-channel method and the impinging stream crushing method. Form micro-bubbles and/or micro-droplets with a diameter of micrometers, and form a microfluidic interface system with other reaction phases, and finally enter the tank reactor to fully react under the action of the catalyst, and undergo subsequent processing to form Different reaction products. The system is in use: the reaction pressure in the tank reactor is 20%-50% of the internal pressure of the existing tank reactor, and the reaction temperature is 87%-90% of the existing reaction temperature, which greatly reduces the reaction The energy consumption and production cost in the process reduce the investment intensity, prolong the equipment operation cycle, ensure the poor intrinsic safety in the reaction process, and effectively ensure the industrialized mass production of the reaction product. It is understandable that the reaction described in this embodiment is a type of reaction in which a tank reactor is used for reaction enhancement. Therefore, the type of catalyst is not specifically limited. It can be an iron-based catalyst, a molybdenum-based catalyst, or a nickel-based catalyst. One or several combinations of cobalt-based catalysts and tungsten-based catalysts, as long as it can ensure the smooth progress of the strengthening reaction. .

Continuing to refer to Figure 2, it is a tubular micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention, which includes: a reactor main body 1 and a micro-interface generator 2; wherein the reactor main body 1 is a tubular reactor for As a reaction chamber for the hydrogenation reaction, to ensure that the hydrogenation reaction can fully proceed; the micro-interface generator 2 is simultaneously arranged at the outer top of the tubular reactor before the gas phase inlet and/or the liquid phase inlet and the tube reactor Internally, used for the hydrogen and liquid and/or solid-liquid mixture materials in the hydrogenation reaction process to transfer the hydrogen and/or liquid phase reactants in the micro-interface generator before entering the reactor body 2. In the second step, it is broken into micro-sized bubbles and/or micro-droplets with a diameter of 1μm≤de<1mm by a preset method, and forms a microfluidic interface system with other reaction phases to increase the gas phase during the hydrogenation reaction. And/or the mass transfer area of the phase boundary between the liquid phase and the liquid phase and/or the solid phase to improve the mass transfer efficiency between the reaction phases, thereby achieving the enhancement of the hydrogenation reaction under the preset temperature and pressure conditions purpose. Specifically, in this embodiment, the hydrogen and liquid and/or solid-liquid mixture materials used as reaction raw materials enter the micro-interface generator 2 before entering the tubular reactor and are broken by microporous aeration or impact The method breaks into micro-bubbles and/or micro-droplets with a diameter of micrometers, and forms a microfluidic interface system with other reaction phases, and finally enters the tubular reactor to fully react under the action of the catalyst, and undergoes subsequent treatment To form different reaction products. The system is in use: the reaction pressure in the tubular reactor is 30%-70% of the existing tubular reactor internal pressure, and the reaction temperature is 91%-94% of the existing reaction temperature, which greatly reduces the reaction temperature. The energy consumption and production cost in the process reduce the investment intensity, prolong the equipment operation cycle, ensure the poor intrinsic safety in the reaction process, and effectively ensure the industrialized mass production of the reaction product. It is understandable that the reaction described in this embodiment is a type of reaction in which a tubular reactor is used for reaction enhancement. Therefore, the type of catalyst is not specifically limited, and it may be an iron-based catalyst, a molybdenum-based catalyst, or a nickel-based catalyst. One or several combinations of cobalt-based catalysts and tungsten-based catalysts, as long as it can ensure the smooth progress of the strengthening reaction.

Continuing to refer to Figure 3, it is a tower type micro-interface strengthening hydrogenation reaction system according to an embodiment of the present invention, which includes: a reactor main body 1 and a micro-interface generator 2; wherein the reactor main body 1 is a tower reactor. Used as a reaction chamber for the hydrogenation reaction to ensure that the hydrogenation is fully carried out; the micro-interface generator 2 is connected to the gas phase inlet and/or the liquid phase inlet on the outside of the lower part of the tower reactor for The hydrogen and liquid and/or solid-liquid mixtures in the hydrogenation reaction process are crushed into the hydrogen and/or liquid phase reactants in the micro-interface generator 2 by a preset method before entering the reactor body. Micron-level micro bubbles and/or micro-droplets with a diameter of 1μm≤de<1mm and form a microfluidic interface system with other reaction phases to increase the gas and/or liquid and liquid phases during the hydrogenation reaction And/or the mass transfer area of the phase boundary between the solid phases, improve the mass transfer efficiency between the reaction phases, and then achieve the purpose of strengthening the hydrogenation reaction under the preset temperature and pressure conditions. Specifically, in this embodiment, before entering the tower reactor, the hydrogen and liquid and/or solid-liquid mixtures used as raw materials for the reaction enter the micro-interface generator 2 through the microporous aeration method and the microfluidic method. One or more methods of Dao method, microfluidic method, pressure field, super-gravity field, ultrasonic field, electromagnetic wave field, impinging stream breaking method, cyclotron shear breaking method, spray method or gas-liquid mixed flow pump method Form micro-bubbles and/or micro-droplets with a diameter of micrometers, and form a microfluidic interface system with other reaction phases, and finally enter the tower reactor to fully react under the action of the catalyst, and undergo subsequent processing to form Different reaction products. During the use of 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 greatly reduces the reaction process. The energy consumption and production cost in the medium, reduce the investment intensity, extend the equipment operation cycle, ensure the poor intrinsic safety in the reaction process, and effectively ensure the industrialized mass production of the reaction product. It is understandable that the reaction described in this embodiment is a type of reaction in which a tower reactor is used for reaction enhancement. Therefore, the type of catalyst is not specifically limited, and it can be an iron-based catalyst, a molybdenum-based catalyst, or a nickel-based catalyst. One or several combinations of cobalt-based catalysts and tungsten-based catalysts, as long as it can ensure the smooth progress of the strengthening reaction.

Continuing to refer to Figure 4, it is a fixed-bed micro-interface intensified hydrogenation reaction system of an embodiment of the present invention, which includes: a reactor body 1 and a micro-interface generator 2; wherein the reactor body 1 is a fixed-bed reactor. Used as a reaction chamber for the hydrogenation reaction to ensure that the hydrogenation reaction can fully proceed; the micro-interface generator 2 is respectively arranged in front of the gas phase inlet and/or the liquid phase inlet on the outer top of the fixed bed reactor. The inside of the fixed-bed reactor is used for the hydrogen and liquid and/or solid-liquid mixture materials in the hydrogenation reaction process to transfer the hydrogen and/or liquid phase reactants in the reactor body before entering the reactor body The micro-interface generator is broken into micro-bubbles and/or micro-droplets with a diameter of micrometers by a preset method, and forms a micro-fluid interface system with other reaction phases to increase the gas phase and/or micro-droplets during the hydrogenation reaction. The mass transfer area of the phase boundary between the liquid phase and the liquid phase and/or the solid phase improves the mass transfer efficiency between the reaction phases, thereby achieving the purpose of strengthening the hydrogenation reaction under the preset temperature and pressure conditions. Specifically, in this embodiment, the hydrogen and liquid and/or solid-liquid mixture materials used as reaction raw materials enter the micro-interface generator 2 before entering the fixed-bed reactor and are broken by micro-channel action or mechanical action. Form micro-sized bubbles and/or micro-droplets with a diameter of 1μm≤de<1mm, and form a microfluidic interface system with other reaction phases, and finally enter the fixed bed reactor to fully react under the action of the catalyst. And after subsequent processing to form different reaction products. During use of this system: the reaction pressure in the fixed bed reactor is 65%-80% of the existing fixed bed reactor internal pressure, and the reaction temperature is 90%-94% of the existing reaction temperature, which greatly reduces the reaction The energy consumption and production cost in the process reduce the investment intensity, prolong the equipment operation cycle, ensure the poor intrinsic safety in the reaction process, and effectively ensure the industrialized mass production of the reaction product. It is understandable that the reaction described in this embodiment is a type of reaction in which a fixed bed reactor is used for reaction enhancement. Therefore, the type of catalyst is not specifically limited. It can be an iron-based catalyst, a molybdenum-based catalyst, or a nickel-based catalyst. One or several combinations of cobalt-based catalysts and tungsten-based catalysts, as long as it can ensure the smooth progress of the strengthening reaction.

Continuing to refer to Figure 5, it is an emulsion bed micro-interface strengthening hydrogenation reaction system of an embodiment of the present invention, which includes: a reactor main body 1 and a micro-interface generator 2; wherein the reactor main body 1 is an emulsion bed reactor. Used as the reaction chamber for the hydrogenation reaction to ensure that the hydrogenation reaction can fully proceed; the micro-interface generator 2 is connected to the gas phase inlet and/or liquid phase inlet on the side of the emulsified bed reactor, and the set number is Two, one of which is arranged outside the emulsified bed reactor, and the other is arranged inside the emulsified bed reactor, for the hydrogen and liquid and/or solid-liquid mixture in the hydrogenation process to enter Before the main body of the reactor, the hydrogen and/or liquid phase reactants are broken into micron-level micro-bubbles and/or micro-liquid with a diameter of 1 μm≤de<1mm in the micro-interface generator 2 by a preset method. Droplets and form a microfluidic interface system with other reaction phases to increase the mass transfer area of the phase boundary between the gas and/or liquid phase and the liquid and/or solid phase during the hydrogenation reaction, and increase the reaction phase The mass transfer efficiency between the two to achieve the purpose of strengthening the hydrogenation reaction under the preset temperature and pressure conditions. Specifically, in this embodiment, before entering the emulsified bed reactor, the hydrogen and liquid and/or solid-liquid mixtures used as raw materials for the reaction enter the micro-interface generator 2 to be broken by mechanical action and field force. Form micro-bubbles and/or micro-droplets with a diameter of micrometers, and form a microfluidic interface system with other reaction phases, and finally enter the emulsified bed reactor to fully react under the action of the catalyst, and undergo subsequent processing to form Different reaction products. During use of this system: the reaction pressure in the emulsified bed reactor is 53%-76% of the internal pressure of the existing emulsified bed reactor, and the reaction temperature is 84%-89% of the existing reaction temperature, which greatly reduces the reaction temperature. The energy consumption and production cost in the process reduce the investment intensity, prolong the equipment operation cycle, ensure the poor intrinsic safety in the reaction process, and effectively ensure the industrialized mass production of the reaction product. It is understandable that the reaction described in this embodiment is a type of reaction in which an emulsion bed reactor is used for reaction enhancement. Therefore, the type of catalyst is not specifically limited. It can be an iron-based catalyst, a molybdenum-based catalyst, or a nickel-based catalyst. One or several combinations of cobalt-based catalysts and tungsten-based catalysts, as long as it can ensure the smooth progress of the strengthening reaction.

Continuing to refer to FIG. 6, it is a suspended bed micro-interface enhanced hydrogenation reaction system according to an embodiment of the present invention, which includes: a reactor body 1 and a micro-interface generator 2; wherein the reactor body 1 is a suspended bed reactor. Used as a reaction chamber for the hydrogenation reaction to ensure that the hydrogenation reaction can fully proceed; the micro-interface generator 2 is connected to the bottom end and the side gas inlet and/or liquid phase inlet of the suspended bed reactor. Before entering the main body of the reactor, the hydrogen and/or liquid and/or solid-liquid mixtures in the hydrogenation reaction process pass the hydrogen and/or liquid phase reactants through a preset in the micro-interface generator. The method breaks into micro-sized bubbles and/or micro-droplets with a diameter of 1μm≤de<1mm, and forms a microfluidic interface system with other reaction phases to increase the gas and/or liquid phase during the hydrogenation reaction The mass transfer area of the phase boundary with the liquid phase and/or the solid phase improves the mass transfer efficiency between the reaction phases, thereby achieving the purpose of strengthening the hydrogenation reaction under the preset temperature and pressure conditions. Specifically, in this embodiment, the hydrogen and liquid and/or solid-liquid mixtures as raw materials for the reaction enter the micro-interface generator 2 before entering the suspended bed reactor through micro-channel action and field force action. It breaks into micro-bubbles and/or micro-droplets with a diameter of micrometers, and forms a microfluidic interface system with other reaction phases, and finally enters the suspended bed reactor to fully react under the action of the catalyst, and undergoes subsequent treatment to Different reaction products are formed. The system is in use: the reaction pressure in the suspended bed reactor is 30%-48% of the existing traditional suspended bed (slurry bed) reactor internal pressure, and the reaction temperature is 78%-84% of the existing reaction temperature , Thereby greatly reducing the energy consumption and production cost in the reaction process, reducing the investment intensity, extending the equipment operation cycle, ensuring the poor intrinsic safety in the reaction process, and effectively ensuring the industrialized large-scale production of the reaction product. It is understandable that the reaction described in this embodiment is a type of reaction in which a suspended bed reactor is used for reaction enhancement. Therefore, the type of catalyst is not specifically limited. It can be an iron-based catalyst, a molybdenum-based catalyst, or a nickel-based catalyst. One or several combinations of cobalt-based catalysts and tungsten-based catalysts, as long as it can ensure the smooth progress of the strengthening reaction.

Continuing to refer to Figure 7, it is a fluidized bed micro-interface strengthening hydrogenation reaction system of an embodiment of the present invention, which includes: a reactor body 1 and a micro-interface generator 2; wherein the reactor body 1 is a fluidized bed reactor, Used as a reaction chamber for the hydrogenation reaction to ensure that the hydrogenation reaction can fully proceed; the micro-interface generator 2 is connected to the gas phase inlet and/or the liquid phase inlet at the bottom and sides of the fluidized bed reactor. Before entering the reactor body, the hydrogen and liquid and/or solid-liquid mixtures in the hydrogenation reaction process pass the hydrogen and/or liquid reactants through the micro-interface generator 2. Suppose the method is broken into micro-sized bubbles and/or micro-droplets with a diameter of 1μm≤de<1mm, and forms a microfluidic interface system with other reaction phases to increase the gas and/or liquid phases during the hydrogenation reaction. The mass transfer area of the phase boundary between the phase and the liquid phase and/or the solid phase improves the mass transfer efficiency between the reaction phases, thereby achieving the purpose of strengthening the hydrogenation reaction under the preset temperature and pressure conditions. Specifically, in this embodiment, the hydrogen and liquid and/or solid-liquid mixtures as raw materials for the reaction enter the micro-interface generator 2 before entering the fluidized bed reactor through micro-channel action and field force action. Or it is broken into micro bubbles and/or micro droplets with a diameter of micrometers under mechanical action, and forms a microfluidic interface system with other reaction phases, and finally enters the fluidized bed reactor to fully react under the action of the catalyst, and After subsequent processing to form different reaction products. During use of this system: the reaction pressure in the fluidized bed reactor is 45%-78% of the internal pressure of the existing fluidized bed reactor, and the reaction temperature is 87%-93% of the existing reaction temperature, which greatly reduces the reaction The energy consumption and production cost in the process reduce the investment intensity, prolong the equipment operation cycle, ensure the poor intrinsic safety in the reaction process, and effectively ensure the industrialized mass production of the reaction product. It is understandable that the reaction described in this embodiment is a type of reaction in which a fluidized bed reactor is used for reaction enhancement. Therefore, the type of catalyst is not specifically limited. It can be an iron-based catalyst, a molybdenum-based catalyst, or a nickel-based catalyst. One or several combinations of cobalt-based catalysts and tungsten-based catalysts, as long as it can ensure the smooth progress of the strengthening reaction.

In addition, the system of the present invention can also be used in various oxidation reactions, chlorination reactions, carbonylation reactions and combustible ice mining and other reaction processes to form micro-interface, micro-nano interface, ultra-micro interface, micro-bubble biochemical reactor or Microbubble bioreactors and other equipment, used micro mixing, micro fluidization, ultra micro fluidization, micro bubble fermentation, micro bubble bubbling, micro bubble mass transfer, micro bubble transfer, micro bubble reaction, micro bubble absorption, micro bubble Oxygen enhancement, microbubble contact and other processes or methods to make the material form multi-phase micro-mixed flow, multi-phase micro-nano flow, multi-phase emulsified flow, multi-phase micro-structured flow, gas-liquid-solid micro-mixed flow, gas-liquid-solid micro-nano flow, Gas-liquid-solid emulsified flow, gas-liquid-solid microstructure flow, microbubble, microbubble flow, microfoam, microfoam flow, microgas liquid flow, gas-liquid micro-nano emulsion flow, ultra micro flow, micro dispersion flow, two micro Mixed flow, micro-turbulent flow, micro-bubble flow, micro-bubble, micro-bubble flow, micro-nano bubble and micro-nano bubble flow and other microfluidics can increase the mass transfer area between phases and improve the reaction efficiency between phases.

Obviously, in the micro-interface intensified hydrogenation reaction system provided by the present invention, by connecting the micro-interface generator to the main body of the reactor, the hydrogen and liquid and/or solid-liquid mixture materials in the hydrogenation reaction process enter the reaction Before the main body of the device, the hydrogen and/or liquid phase reactants are broken into micro bubbles and/or micro bubbles with a diameter of micrometers in the micro-interface generator through mechanical microstructures and/or turbulent microstructures in a preset mode of action. The liquid droplets effectively increase the mass transfer area of the phase boundary between the hydrogen and the liquid and/or solid-liquid mixture during the reaction process, greatly improve the mass transfer efficiency between the reaction phases, and reach the preset pressure range The purpose of internally strengthening the reaction, while greatly reducing the energy consumption and production cost in the reaction process, reducing the investment intensity, extending the equipment operation cycle, ensuring the poor intrinsic safety of the reaction process, and effectively ensuring the industrialization of the reaction product Mass production.

Obviously, those skilled in the art can make various changes and modifications to the present invention without departing from the spirit and scope of the present invention. In this way, if these modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalent technologies, the present invention is also intended to include these modifications and variations.

Claims

A micro-interface strengthening hydrogenation reaction system, which is characterized in that it comprises:

The main body of the reactor is used as a reaction chamber in the hydrogenation reaction process to ensure that the hydrogenation reaction can fully proceed;

A micro-interface generator, which is connected to the main body of the reactor, is used for the hydrogen and liquid and/or solid-liquid mixture material in the hydrogenation reaction process before entering the main body of the reactor to remove the hydrogen and/or In the micro-interface generator, the liquid phase reactant is broken into micro-bubbles and/or micro-droplets with a diameter of micrometers through mechanical micro-structures and/or turbulent micro-structures in a predetermined mode of action, so as to increase the amount of damage during the reaction. The mass transfer area of the phase boundary between the hydrogen and the liquid and/or solid-liquid mixture material improves the mass transfer efficiency between the reaction phases, and strengthens the hydrogenation reaction rate under preset temperature and pressure conditions.
The micro-interface strengthening hydrogenation reaction system according to claim 1, wherein the preset action mode is selected from one or more of microchannel action mode, field force action mode, and mechanical energy action mode; wherein,

The microchannel action mode is to construct the microstructure of the flow channel, so that the gas and/or liquid phase passing through the micro flow channel is broken into micro bubbles and/or micro droplets;

The field force action mode is to use external field force to input energy into the fluid in a non-contact manner to break it into the microbubbles or microdroplets;

The action mode of the mechanical energy is to use the mechanical energy of the fluid to convert it into the surface energy of bubbles or droplets, so that the bubbles or droplets are broken into the microbubbles or microdroplets.
The micro-interface strengthening hydrogenation reaction system according to claim 2, wherein the micro-channel action mode is selected from one of microporous aeration method, micro-nanoporous membrane method, micro-channel method, and microfluidic method. Kind or several.
The micro-interface strengthening hydrogenation reaction system according to claim 2, wherein the field force action mode comprises: pressure field action, supergravity field action, ultrasonic field action or electromagnetic wave field action.
The micro-interface strengthening hydrogenation reaction system according to claim 2, wherein the mechanical energy action mode comprises: impinging stream crushing method, cyclotron shearing crushing method, spray method or gas-liquid mixed flow pump method.
The micro-interface intensified hydrogenation reaction system according to any one of claims 1 to 5, wherein the main body of the reactor comprises: a tank reactor, a tubular reactor, a tower reactor, a fixed bed reactor or Fluidized bed reactor.
The micro-interface intensified hydrogenation reaction system according to claim 6, wherein the micro-interface generator is connected to the gas and/or liquid inlet end of the reactor body, and the number of installations is at least one group .
The micro-interface intensified hydrogenation reaction system according to claim 1, wherein the preset pressure range is 10%-80% of the pressure required by the existing enhanced reaction system.
The micro-interface strengthening hydrogenation reaction system according to claim 8, wherein the micron level range is greater than or equal to 1 μm and less than 1 mm.
The micro-interface intensified hydrogenation reaction system according to any one of claims 1-5 or 7-9, wherein the micro-interface intensified hydrogenation reaction system is applicable to chemical industry, metallurgy, bioengineering, petrochemical industry, medicine , Environmental governance, biochemical fermentation, oil refining, aquaculture, fine chemicals, biological fermentation, and hydrogenation reactions in the fields of mining.