NL2032837B1 - Micro-interfacial strengthening reaction system - Google Patents

Abstract

… The invention discloses a micro-interfacial strengthening reaction system, including: a reactor main body, used as a reaction chamber for gas-liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid and liquid-liquid-solid multiphase reaction medium to ensure the multiphase reaction medium is fully reacted; and a micro-interfacial generator, connected to the reactor main body, used for breaking a gas phase and/or a liquid phase in the multiphase reaction medium into micro-bubbles and/or micro-droplets with a diameter of a micron-order in a predetermined action mode by mechanical microstructures and/or turbulent microstructures in the micro-interfacial generator before the multiphase reaction medium enters the reactor main body, in order to increase a mass transfer area of a phase boundary between the gas phase and/or the liquid phase and a phase boundary between the liquid phase and/or the solid phase, and to improve a mass transfer efficiency between the phases, such that a multiphase reaction is enhanced at a lower predetermined pressure range. The invention effectively solves the problems that the mass transfer rate is affected due to small contact area of the phase boundary of the reaction phase during the use of eXisting reaction strengthening system. 21

Description

MICRO-INTERFACIAL STRENGTHENING REACTION SYSTEM

FIELD OF THE INVENTION

The present invention relates to the technical field of reaction strengthening, in particular to a micro-interfacial strengthening reaction system.

BACKGROUND OF THE INVENTION

An interface refers to a boundary area between one material phase and another material phase.

It exists between these two phases, and its thickness is about a few molecular layers to several tens of molecular layers. The interface is different from the concept of “surface” in geometry. The surface has a thickness and is the boundary area between specific material phases. The interfacial phenomenon occurs along with a mass transfer, and it has a significant impact on the mass transfer process. Extraction, rectification, absorption, gas-liquid reaction, liquid-liquid reaction, and gas- liquid-solid three-phase reaction are all typical interfacial mass transfer processes. Existing multiphase reaction systems have strong adaptability to raw materials and simple operations.

However, due to large sizes of gas and/or liquid in reaction medium, the phase boundary area of gas and/or liquid is relatively small. Therefore, the mass transfer area and the mass transfer rate are severely restricted, which in turn affects the overall efficiency of the reaction. The fundamental reason is that the size of bubbles in the reactor is large (generally 3-30 mm), so the mass transfer area of the gas-liquid phase boundary is small (generally 50-200 m2/m3), thus limiting the mass transfer efficiency. Therefore, high temperature (above 470°C) and high pressure (above 30Mpa) are required to be used in engineering for increasing the mas transfer rate by increasing the solubility of the gas phase and/or liquid phase to, so as to enhance the reaction process. However, high temperature and high pressure produce a series of side effects: high energy consumption and high production cost, high investment intensity, short equipment operation period, many failures, poor intrinsic safety, etc., which bring challenges to industrialized large-scale production.

SUMMARY OF THE INVENTION

In view of this, the present invention proposes a micro-interfacial strengthening reaction system, 1 which aims to solve the problem that the existing strengthening reaction system increases the phase boundary area of each reaction phase by means of high temperature and high pressure during the strengthening reaction process. However, while increasing the mass transfer rate, it is easy to cause problems such as high energy consumption and high production cost, high investment intensity, sort equipment operation period, many failures, poor intrinsic safety, etc., which bring challenges to industrialized large-scale production.

The present invention proposes a micro-interfacial strengthening reaction system, including: a reactor main body, used as a reaction chamber for gas-liquid, liquid-liquid, liquid-solid, gas-liquid- liquid, gas-liquid-solid and liquid-liquid-solid multiphase reaction medium to ensure the multiphase reaction medium is fully reacted; and a micro-interfacial generator, connected to the reactor main body, used for breaking a gas phase and/or a liquid phase in the multiphase reaction medium into micro-bubbles and/or micro-droplets with a diameter of a micron-order in a predetermined action mode by mechanical microstructures and/or turbulent microstructures in the micro-interfacial generator before the multiphase reaction medium enters the reactor main body, in order to increase a mass transfer area of a phase boundary between the gas phase and/or the liquid phase and a phase boundary between the liquid phase and/or the solid phase, and to improve a mass transfer efficiency between the phases, such that a multiphase reaction is enhanced at a predetermined temperature and/or a predetermined pressure range.

Preferably, the predetermined action mode is selected from one or more of a micro-channel action mode, a field force action mode, and a mechanical energy action mode.

The micro-channel action mode utilizes microstructures of a constructed flow channel for breaking the gas phase and/or the liquid phase passing through a micro-channel into the micro- bubbles and/or micro-droplets.

The field force action mode utilizes an external field force action to input energy into the fluid in a non-contact manner for breaking the gas phase and/or the liquid phase into the micro-bubbles and/or micro-droplets.

The mechanical energy action mode converts a mechanical energy of the fluid into a surface energy of bubbles and/or droplets, so that the bubbles and/or droplets are broken into the micro- bubbles and/or micro-droplets. 2

Preferably, the micro-channel action mode is selected from one or more of a group consisting of a machining micro-pore method, a membrane method, a micro-channel method and a micro-fluidic method.

Preferably, the field force action mode comprises: a pressure field action, a supergravity field action, an ultrasonic field action, or an electro-magnetic wave field action.

Preferably, the mechanical energy action mode comprises: an impinging flow crushing method, a cyclone shearing crushing method, a spray method or a gas-liquid mixed flow pump method.

Preferably, the reactor main body comprises: a tank reactor, a tubular reactor, a tower reactor, a fixed-bed reactor or a fluidized-bed reactor.

Preferably, the micro-interfacial generator is connected to an inlet end of the reactor man body, and a number of the micro-interfacial generator is at least one.

Preferably, the predetermined pressure range is 50%-80% of a pressure required for the reaction of an existing enhanced reaction system.

Preferably, a range of the micron-order is greater than or equal to 1pm and less than 1mm.

Preferably, the micro-interfacial strengthening reaction system is applied to fields of chemical industry, metallurgy, bioengineering, petrochemical industry, medicine, environmental treatment, biochemical fermentation, oil refining, aquaculture, fine chemical industry, biological fermentation and mineral exploitation.

Compared with the prior art, the invention has the following beneficial effects:

In the micro-interfacial strengthening reaction system of the present invention, by connecting the micro-interfacial generator on the reactor main body, the gas phase and/or liquid phase in the multiphase reaction medium is broken into micro-bubbles and/or micro-droplets with a diameter of micron-order through a micro-channel action, a field force action or a mechanical energy action before the multiphase reaction medium enters the reactor main body, in order to increase a mass transfer area of a phase boundary between the gas phase and/or the liquid phase and a phase boundary between the liquid phase and/or the solid phase, and to greatly improve a mass transfer efficiency between the phases, thereby achieving the purpose of strengthening the reaction within a preset pressure range. At the same time, the energy consumption and production cost in the reaction process are greatly reduced, the investment intensity is reduced, the equipment operation period is prolonged, the intrinsic safety in the reaction process is ensured, and the industrialized large-scale production of the reaction production is effectively guaranteed.

In particular, the micro-interfacial strengthening reaction system of the present invention can select different crushing methods according to characteristics and process requirements of different reaction phases. For example, the gas phase and/or liquid phase in the reaction medium is broken through a micro-channel action, a field force action or a mechanical energy action, which effectively ensures that the gas phase and/or liquid phase in the reaction medium is effectively broken before the multiphase reaction medium enters the reactor main body. The phase boundary mass transfer efficiency between the gas phase and/or liquid phase and the liquid phase and/or solid phase in the reaction process is ensured, and the reaction efficiency is further improved.

BRIEF DESCRIPTION OF THE DRAWINGS

Upon reading the following detailed description of preferred embodiments, various advantages and benefits will be apparent to those of ordinary skill in the art. The drawings are for the purpose of explaining preferred embodiments only, and do not constitute improper limitations on the present invention. The same components are also denoted by the same reference numerals throughout the drawings. In the drawings:

Fig. 1 is a structural diagram of a tank micro-interfacial strengthening reaction system according to an embodiment of the present invention.

Fig. 2 is a structural diagram of a tubular micro-interfacial strengthening reaction system according to an embodiment of the present invention.

Fig. 3 is a structural diagram of a tower micro-interfacial strengthening reaction system according to an embodiment of the present invention.

Fig. 4 is a structural diagram of a fixed-bed micro-interfacial strengthening reaction system 4 according to an embodiment of the present invention.

Fig. 5 is a structural diagram of an emulsified-bed micro-interfacial strengthening reaction system according to an embodiment of the present invention.

Fig. 6 is a structural diagram of a suspended-bed micro-interfacial strengthening reaction system according to an embodiment of the present invention.

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

In the figure: 1. reactor main body; 2. micro-interfacial generator.

DESCRIPTION OF THE PREFERRED EMBODIMENTS

The technical schemes of the present invention will be clearly and completely described below with reference to the accompanying drawings and specific embodiments, but those skilled in the art will understand that the embodiments described below are part of the embodiments of the present invention, rather than all of the embodiments. It is only used to illustrate the present invention and should not be construed as limiting the scope of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative efforts shall fall within the protection scope of the present invention. If the specific conditions are not indicated in the examples, it is carried out according to the conventional conditions or the conditions suggested by the manufacturer. The reagents or instruments used without the manufacturer's indication are conventional products that can be purchased from the market.

Referring to Figs. 1-7. A micro-interfacial strengthening reaction system according to an embodiment of the present invention is provided, which includes a reactor main body 1 and a micro- interfacial generator (MIG) 2. The reactor main body 1 is used as a reaction chamber for gas-liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid and liquid-liquid-solid multiphase reaction medium to ensure the multiphase reaction medium is fully reacted. The micro-interfacial generator 2 1s connected to the reactor main body 1, and is used for breaking a gas phase and/or a liquid phase in the multiphase reaction medium into micro-bubbles and/or micro-droplets with a diameter of a micron-order in a predetermined action mode by mechanical microstructures and/or turbulent microstructures in the micro-interfacial generator before the multiphase reaction medium 5 enters the reactor main body 1, in order to form micro-interface, micro-nano interface, ultra-micro interface, etc. in other reaction phases, and to form a multiphase fluid formed by micron-scale particles or a multiphase fluid formed by micro-nano-scale particles (referred to as micro-interface fluid) together with other reaction phases, such as multiphase micro-mixed flow, multiphase micro- nano flow, multiphase emulsification flow, multiphase micro-structure flow, gas-liquid-solid micro- mixed flow, gas-liquid-solid micro-nano flow, gas-liquid-solid emulsion flow, gas-liquid-solid micro- structure flow, micro-bubble, micro-bubble flow, micro-foam, micro-foam flow, micro-gas-liquid flow, gas-liquid micro-nano emulsion flow, ultra-micro flow, micro-dispersed flow, two micro-mixed flow, micro-turbulent flow, micro-bubble flow, micro-bubble, micro-bubble flow, micro-nano bubble and micro-nano bubble flow, etc, thereby effectively increasing the phase boundary mass transfer area between the gas and/or liquid phase and the liquid and/or solid phase during the reaction process, and greatly improving the mas transfer efficiency between the reaction phases. Finally, the objective of strengthening multiple reactions under lower preset temperature and pressure conditions is achieved. At the same time, it effectively solves problems of high temperature, high pressure, high material consumption, high investment, and high safety risks in traditional gas-liquid and gas-liquid- solid multiphase hydrogenation processes. As a result, the investment and operation costs of equipment are significantly reduced.

In this embodiment, the multiphase medium, such as gas-liquid, liquid-liquid, liquid-solid, gas- liquid-liquid, gas-liquid-solid, and liquid-liquid-solid as reaction raw materials, first enters the micro- interfacial generator 2 before it enters the reactor main body 1. Through internal mechanical micro- structures and/or turbulent micro-structures, the liquid and/or gas in the multiphase reaction medium is broken into micro-bubbles and/or micro-droplets with a diameter of 1 um < de <Imm by means of a micro-channel action, a field force action or a mechanical energy action, thereby forming micro- interface, micro-nano interface or ultra-micro interface, etc. Then, it is fully mixed with other reaction phases such as multiphase micro-mixed flow, multiphase micro-nano flow, multiphase emulsification flow, multiphase micro-structure flow, gas-liquid-solid micro-mixed flow, gas-liquid-solid micro- nano flow, gas-liquid-solid emulsion flow, gas-liquid-solid micro-structure flow, micro-bubble, micro-bubble flow, micro-foam, micro-foam flow, micro-gas-liquid flow, gas-liquid micro-nano emulsion flow, ultra-micro flow, micro-dispersed flow, two micro-mixed flow, micro-turbulent flow, micro-bubble flow, micro-bubble, micro-bubble flow, micro-nano bubble and micro-nano bubble 6 flow, etc. to form a micro-interfacial fluid reaction system. Finally, it enters the reactor main body 1 through the feed port of the reactor main body 1 and fully reacts under action of catalysts, and undergoes subsequent treatments to form different reaction products, thereby effectively increasing the mass transfer area of the phase boundary between the gas phase and/or the liquid phase and the liquid phase and/or the solid phase during the reaction process, and further improving the mass transfer efficiency between the reaction phases during the reaction process. Finally, the purpose of strengthening the reaction within 10%-80% of the pressure required for the reaction of the existing strengthening reaction system is achieved. At the same time, it effectively solves the problems of high temperature, high pressure, high material consumption, high investment and high safety risk in traditional gas-liquid and gas-liquid-solid multiphase hydrogenation reaction processes, thereby significantly reducing the investment cost and operating cost of the equipment.

Specifically, the reactor main body 1, as the main place where each reaction raw material reacts in the reaction process, has a shell structure as a whole, which can be: a tank reactor, a tubular reactor, a tower reactor, a fixed-bed reactor or a fluidized-bed reactor, as long as the reaction chamber for the multiphase reaction medium to ensure that the multiphase reaction medium can be fully reacted. The fluidized-bed reactor can choose any form of reactor such as an emulsified-bed reactor, a suspended- bed, and a fluidized-bed reactor according to different reaction phases in the reaction raw materials.

In this embodiment, the specific type and structure of the reactor main body 1 can be selected or designed according to different fields of use, such as chemical, metallurgy, bioengineering, petrochemical, pharmaceutical, environmental treatment, biochemical fermentation, oil refining, aquaculture, fine chemical, biological fermentation and mineral mining, etc., process parameters such as reaction temperature and reaction pressure, as well as parameters as quality requirements of reaction products. As long as it can ensure that use requirements are met to the greatest extent during the reaction process, that is, to maximize the reaction rate, improve the quality of finished products, reduce cost, and ensure safe operations. It can be understood that the specific structure of the reactor main body 1 must be different to a certain extent in different fields or different reaction processes, for example, disposing positions and numbers of inlet ports and outlet ports are different.

Specifically, the micro-interfacial generator 2 is used as a core device for breaking the gas and/or liquid in the multiphase reaction medium during the reaction process. It is provided with a gas-phase 7 and/or liquid-phase feed port on the reactor main body 1, and the gas phase and/or liquid phase in the multiphase reaction medium is passed through a mechanical micro-structure and/or a turbulent micro- stricture, in order to convert the mechanical energy of the gas phase and/or liquid phase into the surface energy of the gas phase and/or liquid phase during the multiphase reaction by means of a micro-channel action, a field force action or a mechanical energy action, etc., then break the gas phase and/or liquid phase into micron-scale micro-bubbles and/or micro-droplets with a diameter of 1 wm < de <1mm, and form a micro-fluidic interfacial system with other reaction phases, thereby effectively increasing the phase boundary mass transfer area between the gas phase and/or liquid phase and the liquid phase an/or solid phase and the liquid phase an/or solid phase during the reaction process, which greatly improves the mass transfer efficiency between the reaction phases. Finally, the purpose of strengthening the multiple reactions under lower preset temperature and pressure conditions is achieved. At the same time, it effectively solves problems of high temperature, high pressure, high material consumption, high investment and high safety risk in traditional gas-liquid and gas-liquid- solid multiphase hydrogenation reaction process, thereby significantly reducing the investment cost and operating cost of equipment.

In this embodiment, the micro-interfacial generator 2 is connected to the feed ports of the reactor main body 1, and the specific position and quantity of the micro-interfacial generator 2 can be determined according to the specific position and quantity of the gas phase and/or liquid phase feed ports on the reactor main body 1. For example, it can be individually arranged on the top, bottom, or side of the reactor main body 1 to form a corresponding top-mounted, bottom-mounted or side- mounted micro-interfacial strengthening reaction system, or it can be placed on the top, bottom and side of the reactor main body 1 at the same time in order to form a variety of hedging micro-interfacial strengthening reaction systems. Meanwhile, the micro-interfacial generator 2 is disposed inside and/or outside the reactor main body 1. In particular, the specific mode that the micro-interfacial generator 2 breaks the gas phase and/or liquid phase in the multiphase reaction process can also be selected according to specific process requirements, it can select from one or more of a micro-channel action mode, a field force action mode, and a mechanical energy action mode. The micro-channel action mode utilizes micro-structures of a constructed flow channel for breaking the gas phase and/or the liquid phase passing through a micro-channel into the micro-bubbles and/or micro-droplets. For example, a micro-porous ventilation method, a micro-nano porous membrane method (various metal 8 membranes, inorganic membranes or organic membranes), a micro-channel method and a micro- fluidic method. The field force action mode utilizes an external field force action to input energy into the fluid in a non-contact manner for breaking the gas phase and/or the liquid phase into the micro- bubbles and/or micro-droplets. The mechanical energy action mode converts a mechanical energy of the fluid into a surface energy of bubbles and/or droplets, so that the bubbles and/or droplets are broken into the micro-bubbles and/or micro-droplets, which includes: an impinging flow crushing method, a cyclone shearing crushing method, a spray method or a gas-liquid mixed flow pump method, etc. During the process of use, before the multiphase reaction medium required for the reaction enters the reactor main body 1, the multiphase reaction medium is broken into micron-order micro-bubbles and/or micron-droplets with a diameter of 1 ‚4m < de <Imm to form micro-interfaces, micro-nano interfaces or ultra-micro interfaces, etc., by means of the micro-channel action mode, the field force action mode or mechanical energy mode, etc. Hence, the mass transfer area of the phase boundary between the gas phase and/or liquid phase and the liquid phase and/or solid phase is effectively increased during the reaction process, thereby improving the mass transfer efficiency between the reaction phases during the reaction process. Finally, the purpose of strengthening the reaction within 10%-80% of the pressure required for the reaction of the existing strengthening reaction system is achieved. At the same time, it effectively solves the problems of high temperature, high pressure, high material consumption, high investment and high safety risk in traditional gas- liquid and gas-liquid-solid multiphase hydrogenation reaction processes, thereby significantly reducing the investment cost and operating cost of the equipment.

Please continue to refer to Fig. 1. Fig. 1 is a structural diagram of a tank micro-interfacial strengthening reaction system according to an embodiment of the present invention, which includes a reactor main body 1 and a micro-interfacial generator 2. The reactor main body 1 is a tank reactor, which is used as the reaction chamber of multiphase reaction medium such as gas-liquid, liquid- liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid and liquid-liquid-solid, to ensure that the multiphase reaction medium can fully react. The micro-interfacial generator 2 is connected to the gas- phase inlet and/or the liquid-phase inlet of the outer side of the tank reactor, and the number of the micro-interfacial generator 2 is one. Before the multiphase reaction medium enters the tank reactor, the micro-interfacial generator 2 1s used to crush the gas phase and/or liquid phase in the multiphase reaction medium into micro-bubbles and/or micro-droplets with a diameter of 1 ym < de < Imm 9 through a preset method, and form a micro-fluidic interfacial system with other reaction phases, so as to increase the mass transfer area of the phase boundary between the gas phase and/or liquid phase and the liquid phase and/or solid phase during the reaction process, and improve the mass transfer efficiency between the reaction phases, thereby achieving the purpose of strengthening multiple reactions under preset temperature and pressure conditions. In this embodiment, before the multiphase medium, such as gas-liquid, liquid-liquid, gas-liquid-liquid, liquid-solid, gas-liquid-solid, and liquid-liquid-solid, as reaction raw materials enters the tank reactor, it first enters the micro- interfacial generator 2 and is broken into micro-bubbles and/or micro-droplets with a diameter of microns by the micro-channel method and the impinging flow breaking method, and forms a micro- fluid interfacial system with other reaction phases. Finally, it enters into the tank reactor for full reaction under the action of catalysts, and undergoes subsequent treatments to form different reaction products. During the use process of the this system: the reaction pressure in the tank reactor is 20%- 50% of the internal pressure of the existing tank reactor, and the reaction temperature is 87%-90% of the existing reaction temperature, which greatly reduces energy consumption and production costs in the reaction process, reduces investment intensity, prolongs the equipment operation period, and guarantees the intrinsic safety in the reaction process, such that the industrialized large-scale production of the reaction products is effectively guaranteed. It can be understood that, the reaction in this embodiment is a type of reaction in which a tank reactor is used for reaction strengthening, so the type of catalyst is not specifically limited. It can be one or a combination of iron-based catalysts, molybdenum-based catalysts, nickel-based catalysts, cobalt-based catalysts, and tungsten-based catalysts, as long as the strengthening reaction can be ensured smoothly.

Please continue to refer to Fig. 2. Fig. 2 is a structural diagram of a tubular micro-interfacial strengthening reaction system according to an embodiment of the present invention, which includes a reactor main body 1 and a micro-interfacial generator 2. The reactor main body 1 1s a tubular reactor, which is used as the reaction chamber for gas-liquid or liquid-liquid two-phase reaction medium to react, so as to ensure that the gas-liquid or liquid-liquid two-phase reaction medium can fully react.

The micro-interfacial generators 2 are simultaneously arranged in front of the gas-phase inlet and/or the liquid-phase inlet of the outer top of the tubular reactor and the interior of the tubular reactor.

Before the gas-liquid or liquid-liquid two-phase reaction medium enters the tubular reactor, the micro-interfacial generator 2 is used to crush the gas phase and/or liquid phase in the gas-liquid or 10 liquid-liquid two-phase reaction medium into micro-bubbles and/or micro-droplets with a micron- order through a preset method, and form a micro-fluidic interfacial system with other reaction phases, in order to increase the mass transfer area of the phase boundary between the gas phase and/or liquid phase and the liquid phase and/or solid phase during the reaction process, and improve the mass transfer efficiency between the reaction phases, thereby achieving the purpose of strengthening multiple reactions under preset temperature and pressure conditions. Specifically, in this embodiment, before the gas-liquid or liquid-liquid two-phase reaction medium as reaction raw materials enters the tubular reactor, it first enters the micro-interfacial generator 2 and is broken into micro-bubbles and/or micro-droplets with a diameter of 1 4m < de < 1 mm by the micro-pore ventilation method or the impact crushing method, and forms a micro-fluid interfacial system with other reaction phases.

Finally, it enters into the tubular reactor for full reaction under the action of catalysts, and undergoes subsequent treatments to form different reaction products. During the use process of the this system: the reaction pressure in the tubular reactor is 30%-70% of the internal pressure of the existing tubular reactor, and the reaction temperature is 91%-94% of the existing reaction temperature, which greatly reduces energy consumption and production costs in the reaction process, reduces investment intensity, prolongs the equipment operation period, and guarantees the intrinsic safety in the reaction process, such that the industrialized large-scale production of the reaction products is effectively guaranteed. It can be understood that, the reaction in this embodiment is a type of reaction in which a tubular reactor is used for reaction strengthening, so the type of catalyst is not specifically limited.

It can be one or a combination of iron-based catalysts, molybdenum-based catalysts, nickel-based catalysts, cobalt-based catalysts, and tungsten-based catalysts, as long as the strengthening reaction can be ensured smoothly.

Please continue to refer to Fig. 3. Fig. 3 is a structural diagram of a tower micro-interfacial strengthening reaction system according to an embodiment of the present invention, which includes areactor main body 1 and a micro-interfacial generator 2. The reactor main body 1 is a tower reactor, which is used as the reaction chamber of multiphase reaction medium, such as gas-liquid, liquid- liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid and liquid-liquid-solid, to ensure that the multiphase reaction medium can fully react. The micro-interfacial generator 2 is connected in front of the gas phase inlet and/or the liquid phase inlet outside the lower part of the tower reactor. Before the multiphase reaction medium enters the tower reactor, the micro-interfacial generator 2 is used to 11 crush the gas phase and/or liquid phase in the multiphase reaction medium into micro-bubbles and/or micro-droplets with a diameter of 1 zm < de < Imm through a preset method, and form a micro- fluidic interfacial system with other reaction phases, in order to increase the mass transfer area of the phase boundary between the gas phase and/or liquid phase and the liquid phase and/or solid phase during the reaction process, and improve the mass transfer efficiency between the reaction phases, thereby achieving the purpose of strengthening multiple reactions under preset temperature and pressure conditions. Specifically, in this embodiment, before the gas-liquid or liquid-liquid two-phase medium as reaction raw materials enters the tower reactor, it first enters the micro-interfacial generator 2 and is broken into micro-bubbles and/or micro-droplets with a diameter of microns by

IO means of the micro-porous ventilation method, the membrane method (various metal membranes, inorganic membranes or organic membranes), the micro-channel method, micro-fluidic method, the pressure field method, the hyper-gravity field method, the ultrasonic field method, the electromagnetic wave field method, the impinging flow crushing method, the cyclone shearing crushing method, the spray method or the gas-liquid mixed flow pump method, and forms a micro- fluid interfacial system with other reaction phases. Finally, it enters into the interior of the tower reactor for full reaction under the action of catalysts, and undergoes subsequent treatments to form different reaction products. During the use of the 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 energy consumption and production costs in the reaction process, reduces investment intensity, prolongs the equipment operation period, and guarantees the intrinsic safety in the reaction process, such that the industrialized large-scale production of the reaction products is effectively guaranteed. It can be understood that, the reaction in this embodiment is a type of reaction in which a tower reactor 1s used for reaction strengthening, so the type of catalyst is not specifically limited. It can be one or a combination of iron-based catalysts, molybdenum-based catalysts, nickel-based catalysts, cobalt- based catalysts, and tungsten-based catalysts, as long as the strengthening reaction can be ensured smoothly.

Please continue to refer to Fig. 4. Fig. 4 is a structural diagram of a fixed-bed micro-interfacial strengthening reaction system according to an embodiment of the present invention, which includes a reactor main body 1 and a micro-interfacial generator 2. The reactor main body 1 is a fixed-bed 12 reactor, which is used as the reaction chamber of multiphase reaction medium, such as gas-liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid and liquid-liquid-solid, to ensure that the multiphase reaction medium can fully react. The micro-interfacial generators 2 are respectively arranged in front of the gas phase inlet and/or the liquid phase inlet of the outer top of the fixed-bed reactor and the interior of the fixed-bed reactor. Before the multiphase reaction medium enters the fixed-bed reactor, the micro-interfacial generator 2 is used to crush the gas phase and/or liquid phase in the multiphase reaction medium into micro-bubbles and/or micro-droplets with a diameter of micron-order through a preset method, and form a micro-fluidic interfacial system with other reaction phases, in order to increase the mass transfer area of the phase boundary between the gas phase and/or liquid phase and the liquid phase and/or solid phase during the reaction process, and improve the mass transfer efficiency between the reaction phases, thereby achieving the purpose of strengthening multiple reactions under preset temperature and pressure conditions. Specifically, in this embodiment, before the gas-liquid or liquid-liquid two-phase medium as reaction raw materials enters the fixed- bed reactor, it first enters the micro-interfacial generator 2 and is broken into micro-bubbles and/or micro-droplets with a diameter of 1 zm < de < Imm by means of the micro-channel action or the mechanical action, and forms a micro-fluid interfacial system with other reaction phases. Finally, it enters into the interior of the fixed-bed reactor for full reaction under the action of catalysts, and undergoes subsequent treatments to form different reaction products. During the use of the this system: the reaction pressure in the fixed-bed reactor is 65%-80% of the internal pressure of the existing fixed-bed reactor, and the reaction temperature is 90%-94% of the existing reaction temperature, which greatly reduces energy consumption and production costs in the reaction process, reduces investment intensity, prolongs the equipment operation period, and guarantees the intrinsic safety in the reaction process, such that the industrialized large-scale production of the reaction products 1s effectively guaranteed. It can be understood that, the reaction in this embodiment is a type of reaction in which a fixed-bed reactor is used for reaction strengthening, so the type of catalyst is not specifically limited. It can be one or a combination of iron-based catalysts, molybdenum-based catalysts, nickel-based catalysts, cobalt-based catalysts, and tungsten-based catalysts, as long as the strengthening reaction can be ensured smoothly.

Please continue to refer to Fig. 5. Fig. 5 is a structural diagram of an emulsified-bed micro- interfacial strengthening reaction system according to an embodiment of the present invention, which 13 includes a reactor main body 1 and a micro-interfacial generator 2. The reactor main body 1 is an emulsified-bed reactor, which is used as the reaction chamber of multiphase reaction medium, such as gas-liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid and liquid-liquid-solid, to ensure that the multiphase reaction medium can fully react. The micro-interfacial generator 2 is connected to the gas phase inlet and/or the liquid phase inlet of the side the emulsified-bed reactor, and the number is two, wherein one of which is arranged outside the emulsified-bed reactor, and the other is arranged inside the emulsified-bed reactor. Before the multiphase reaction medium enters the emulsified-bed reactor, the micro-interfacial generator 2 is used to crush the gas phase and/or liquid phase in the multiphase reaction medium into micro-bubbles and/or micro-droplets with a diameter of 1 gm <de < Imm through a preset method, and form a micro-fluidic interfacial system with other reaction phases, in order to increase the mass transfer area of the phase boundary between the gas phase and/or liquid phase and the liquid phase and/or solid phase during the reaction process, and improve the mass transfer efficiency between the reaction phases, thereby achieving the purpose of strengthening multiple reactions under preset temperature and pressure conditions. Specifically, in this embodiment, before the gas-liquid or liquid-liquid two-phase medium as reaction raw materials enters the emulsified-bed reactor, it first enters the micro-interfacial generator 2 and is broken into micro-bubbles and/or micro-droplets with a diameter of microns by means of the mechanical action and the field force action, and forms a micro-fluid interfacial system with other reaction phases.

Finally, it enters into the interior of the emulsified-bed reactor for full reaction under the action of catalysts, and undergoes subsequent treatments to form different reaction products. During the use of the 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 energy consumption and production costs in the reaction process, reduces investment intensity, prolongs the equipment operation period, and guarantees the intrinsic safety in the reaction process, such that the industrialized large-scale production of the reaction products is effectively guaranteed. It can be understood that, the reaction in this embodiment is a type of reaction in which an emulsified-bed reactor is used for reaction strengthening, so the type of catalyst is not specifically limited. It can be one or a combination of iron-based catalysts, molybdenum-based catalysts, nickel-based catalysts, cobalt-based catalysts, and tungsten-based catalysts, as long as the strengthening reaction can be ensured smoothly. 14

Please continue to refer to Fig. 6. Fig. 6 is a structural diagram of a suspended-bed micro- interfacial strengthening reaction system according to an embodiment of the present invention, which includes a reactor main body 1 and a micro-interfacial generator 2. The reactor main body 1 is a suspended-bed reactor, which is used as the reaction chamber of multiphase reaction medium, such as gas-liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid and liquid-liquid-solid, to ensure that the multiphase reaction medium can fully react. The micro-interfacial generators 2 are connected to the gas phase inlet and/or the liquid phase inlet of the bottom end and the side of the suspended-bed reactor, and the number of the micro-interfacial generator 2 is two. The micro- interfacial generator 2 located at the side of the suspended-bed reactor is connected to the outside of the suspended-bed reactor, and the micro-interfacial generator 2 located at the bottom end is connected to the interior of the suspended-bed reactor. Before the multiphase reaction medium enters the suspended-bed reactor, both the micro-interfacial generators 2 are used to crush the gas phase and/or liquid phase in the multiphase reaction medium into micro-bubbles and/or micro-droplets with a diameter of | 41m S de < 1 mm through a preset method, and form a micro-fluidic interfacial system with other reaction phases, in order to increase the mass transfer area of the phase boundary between the gas phase and/or liquid phase and the liquid phase and/or solid phase during the reaction process, and improve the mass transfer efficiency between the reaction phases, thereby achieving the purpose of strengthening multiple reactions under preset temperature and pressure conditions.

Specifically, in this embodiment, before the gas-liquid or liquid-liquid two-phase medium as reaction raw materials enters the suspended-bed reactor, it first enters the micro-interfacial generator 2 and is broken into micro-bubbles and/or micro-droplets with a diameter of a micron-order by means of the micro-channel action or the field force action, and forms a micro-fluid interfacial system with other reaction phases. Finally, it enters into the interior of the suspended-bed reactor for full reaction under the action of catalysts, and undergoes subsequent treatments to form different reaction products.

During the use of the this system: the reaction pressure in the suspended-bed reactor is 30%-48% of the internal pressure of the existing suspended-bed reactor, and the reaction temperature is 78%-84% of the existing reaction temperature, which greatly reduces energy consumption and production costs in the reaction process, reduces investment intensity, prolongs the equipment operation period, and guarantees the intrinsic safety in the reaction process, such that the industrialized large-scale production of the reaction products is effectively guaranteed. It can be understood that, the reaction 15 in this embodiment is a type of reaction in which a suspended-bed reactor is used for reaction strengthening, so the type of catalyst is not specifically limited. It can be one or a combination of iron-based catalysts, molybdenum-based catalysts, nickel-based catalysts, cobalt-based catalysts, and tungsten-based catalysts, as long as the strengthening reaction can be ensured smoothly.

Please continue to refer to Fig. 7. Fig. 7 1s a structural diagram of a fluidized-bed micro- interfacial strengthening reaction system according to an embodiment of the present invention, which includes a reactor main body 1 and a micro-interfacial generator 2. The reactor main body 1 is a fluidized-bed reactor, which is used as the reaction chamber of multiphase reaction medium, such as gas-liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid and liquid-liquid-solid, to ensure that the multiphase reaction medium can fully react. The micro-interfacial generators 2 are connected to the gas phase inlet and/or the liquid phase inlet of the bottom end and the side of the fluidized-bed reactor, and the number of the micro-interfacial generator 2 is two. The micro- interfacial generator 2 located at the side of the fluidized-bed reactor 1s connected to the interior of the fluidized-bed reactor, and the micro-interfacial generator 2 located at the bottom end is connected to the outside of the fluidized-bed reactor. Before the multiphase reaction medium enters the fluidized-bed reactor, both the micro-interfacial generators 2 are used to crush the gas phase and/or liquid phase in the multiphase reaction medium into micro-bubbles and/or micro-droplets with a diameter of 1 4m = de <1 mm through a preset method, and form a micro-fluidic interfacial system with other reaction phases, in order to increase the mass transfer area of the phase boundary between the gas phase and/or liquid phase and the liquid phase and/or solid phase during the reaction process, and improve the mass transfer efficiency between the reaction phases, thereby achieving the purpose of strengthening multiple reactions under preset temperature and pressure conditions.

Specifically, in this embodiment, before the gas-liquid or liquid-liquid two-phase medium as reaction raw materials enters the fluidized-bed reactor, it first enters the micro-interfacial generators 2 and is broken into micro-bubbles and/or micro-droplets with a diameter of a micron-order by means of the micro-channel action, the field force action, or the mechanical action, and forms a micro-fluid interfacial system with other reaction phases. Finally, it enters into the interior of the fluidized-bed reactor for full reaction under the action of catalysts, and undergoes subsequent treatments to form different reaction products. During the use of the 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 16 temperature 1s 87%-93% of the existing reaction temperature, which greatly reduces energy consumption and production costs in the reaction process, reduces investment intensity, prolongs the equipment operation period, and guarantees the intrinsic safety in the reaction process, such that the industrialized large-scale production of the reaction products is effectively guaranteed. It can be understood that, the reaction in this embodiment is a type of reaction in which a fluidized-bed reactor is used for reaction strengthening, so the type of catalyst is not specifically limited. It can be one or a combination of iron-based catalysts, molybdenum-based catalysts, nickel-based catalysts, cobalt- based catalysts, and tungsten-based catalysts, as long as the strengthening reaction can be ensured smoothly.

Furthermore, the system of the present invention can be adopted in various reaction processes such as hydrogenation reaction, oxidation reaction, chlorination reaction, carbonylation reaction and combustible ice mining, thereby forming equipment such as micro-interface reactors, micro-nano interface reactors, ultra-micro interface reactors, micro-bubble biochemical reactors, or micro-bubble bioreactor. Through processes or methods such as 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 oxygenation, micro- bubble contact, the material can form micro-fluidics such as multiphase micro-mixed flow, multiphase micro-nano flow, multiphase emulsification flow, multiphase micro-structure flow, gas- liquid-solid micro-mixed flow, gas-liquid-solid micro-nano flow, gas-liquid-solid emulsion flow, gas- liquid-solid micro-structure flow, micro-bubble, micro-bubble flow, micro-foam, micro-foam flow, micro-gas-liquid flow, gas-liquid micro-nano emulsion flow, ultra-micro flow, micro-dispersed flow, two micro-mixed flow, micro-turbulent flow, micro-bubble flow, micro-bubble, micro-bubble flow, micro-nano bubble and micro-nano bubble flow, etc., thereby effectively increasing the mass transfer area between the phases to further improve the mass transfer efficiency between the reaction phases.

Obviously, by connecting the micro-interfacial generator to the reactor main body in the micro- interfacial strengthening reaction system of the present invention, the gas and/or liquid in the multiphase reaction medium is broken into micro-bubbles and/or micro-droplets with a diameter of a micron-order by means of a micro-channel action, a field force action or a mechanical energy action in the micro-interfacial generator before the multiphase reaction medium enters the reactor main body, in order to increase the mass transfer area of the phase boundary between the gas phase, liquid 17 phase and/or gas phase, liquid phase and solid phase during the reaction process, and greatly improve the mass transfer efficiency between the reaction phases during the reaction process, thereby achieving the purpose of strengthening multiple reactions under a preset pressure.

In particular, the micro-interfacial strengthening reaction system of the present invention can select different micro-interfacial generators according to their own characteristics and process requirements of different reaction phases, and then different crushing methods can be selected. For example, the gas phase and/or liquid phase in the reaction medium is broken through a micro-channel action, a field force action or a mechanical energy action, which effectively ensures that the gas phase and/or liquid phase in the reaction medium is effectively broken before the multiphase reaction medium enters the reactor main body. The effectiveness of the fragmentation of the gas and/or liquid in the reaction medium before the multiphase reaction medium enters the reactor main body is effectively ensured, the phase boundary mass transfer efficiency between the gas phase, liquid phase and/or the gas phase, liquid phase and solid phase in the reaction process is ensured, and the reaction efficiency is further improved.

Certainly, various modifications and variations can be made in the present invention by those skilled in the art without departing from the spirt and scope of the invention. Thus, these modification, and variations of the present invention shall fall within the protection scope of the claims of the present invention and their equivalents, and the present invention is also intended to include these modifications and variations. 18

Claims (8)

ConclusiesConclusions 1. Een micro-grensvlakversterkend reactiesysteem, bestaande uit: een reactorhoofdlichaam, dat wordt gebruikt als reactiekamer voor gas-vloeistof, vloeistof- vloeistof, vloeibare-vaste stof, gas-vloeistof-vloeistof, gas-vloeistof-vaste stof en vloeistof-vloeistof- vaste stof meerfasig reactiemedium om ervoor te zorgen dat het meerfasig reactiemedium volledig reageert; en een micro-grensvlakgenerator, verbonden met het hoofdlichaam van de reactor, die wordt gebruikt voor het breken van een gasfase en/of een vloeibare fase in het meerfasig reactiemedium in microbellen en/of microdruppels met een diameter van een micronvolgorde in een vooraf bepaalde werkingsmodus door mechanische microstructuren en/of turbulente microstructuren in de micro- grensvlakgenerator voordat het meerfasig reactiemedium het hoofdlichaam van de reactor binnendringt, om een massaoverdrachtsgebied van een fasegrens tussen de gasfase en/of de vloeibare fase en een fasegrens tussen de vloeibare fase en/of de vaste fase te vergroten en een massaoverdrachtsefficiéntie tussen de fasen te verbeteren, zodat een meerfasige reactie wordt versterkt bij een vooraf bepaalde temperatuur en/of een vooraf bepaald drukbereik.1. A micro-interfacial strengthening reaction system, consisting of: a reactor main body, which is used as a reaction chamber for gas-liquid, liquid-liquid, liquid-solid, gas-liquid-liquid, gas-liquid-solid and liquid-liquid- solid multiphase reaction medium to ensure that the multiphase reaction medium reacts completely; and a micro-interfacial generator, connected to the main body of the reactor, which is used to break a gas phase and/or a liquid phase in the multiphase reaction medium into microbubbles and/or microdroplets of micron order in diameter in a predetermined operating mode by mechanical microstructures and/or turbulent microstructures in the interfacial microgenerator before the multiphase reaction medium enters the main body of the reactor, to form a mass transfer region of a phase boundary between the gas phase and/or the liquid phase and a phase boundary between the liquid phase and/or the solid phase and improve mass transfer efficiency between the phases, so that a multiphase reaction is enhanced at a predetermined temperature and/or a predetermined pressure range. 2. Het micro-grensvlakversterkend reactiesysteem volgens claim 1, waarbij de vooraf bepaalde werkingsmodus wordt gekozen uit een of meer van een microkanaalwerkingsmodus, een veldkrachtwerkingsmodus en een mechanische energiewerkingsmodus; waarin: de microkanaalwerkingsmodus maakt gebruik van microstructuren van een geconstrueerd stroomkanaal voor het breken van de gasfase en/of de vloeibare fase die door een microkanaal in de microbellen en/of microdruppels overgaat; de veldkrachtwerkingsmodus maakt gebruik van een externe veldkrachtwerking om op een contactloze manier energie in de vloeistof in te voeren voor het breken van de gasfase en/of de vloeibare fase in de microbellen en/of microdruppels; en de mechanische energiewerkingsmodus zet een mechanische energie van de vloeistof om in een oppervlakte-energie van bellen en/of druppels, zodat de bellen en/of druppels in de microbellen en/of 19 microdruppels worden gebroken.2. The micro-interfacial strengthening reaction system according to claim 1, wherein the predetermined mode of operation is selected from one or more of a micro-channel mode of operation, a field force mode of operation and a mechanical energy mode of operation; wherein: the microchannel mode of operation uses microstructures of an engineered flow channel to break the gas phase and/or the liquid phase passing through a microchannel into the microbubbles and/or microdroplets; the field force operation mode uses an external field force action to introduce energy into the liquid in a contactless manner for breaking the gas phase and/or the liquid phase in the microbubbles and/or microdroplets; and the mechanical energy operation mode converts a mechanical energy of the liquid into a surface energy of bubbles and/or drops, so that the bubbles and/or drops are broken into the microbubbles and/or 19 microdrops. 3. Het micro-grensvlakversterkend reactiesysteem volgens claim 2, waarbij de microkanaal werkingsmodus wordt gekozen uit een of meer van een groep bestaande uit een machinale bewerking van microporiën, een membraanmethode, een microkanaalmethode en een microfluïdetische methode.3. The micro-interfacial strengthening reaction system according to claim 2, wherein the microchannel mode of operation is selected from one or more of a group consisting of a micropore machining method, a membrane method, a microchannel method and a microfluidic method. 4. Het micro-grensvlakversterkend reactiesysteem volgens clam 2, waarbij de veldkrachtwerkingsmodus bestaat uit: een drukveldactie, een superzwaartekrachtveldactie, een ultrasone veldwerking of een elektromagnetische golfveldactie.4. The micro-interfacial strengthening reaction system according to clam 2, wherein the field force operation mode consists of: a pressure field action, a supergravity field action, an ultrasonic field action or an electromagnetic wave field action. 5. Het micro-grensvlakversterkend reactiesysteem volgens claim 2, waarbij de mechanische energiewerkingsmodus bestaat uit: een methode voor het breken met botsende stroom, een methode voor het breken met cycloonafschuifkrachten, een sproeimethode of een pompmethode met een gas- vloeistof-gemengde stroom.5. The micro-interfacial strengthening reaction system according to claim 2, wherein the mechanical energy operation mode consists of: an impinging flow fracturing method, a cyclone shear fracturing method, a spraying method or a gas-liquid mixed flow pumping method. 6. Het micro-grensvlakversterkend reactiesysteem volgens een van de claims 1-5, waarbij het hoofdlichaam van de reactor bestaat uit: een tankreactor, een buisvormige reactor, een torenreactor, een reactor met een vast bed of een reactor met een wervelbed.6. The micro-interfacial strengthening reaction system according to any of claims 1-5, wherein the main body of the reactor consists of: a tank reactor, a tubular reactor, a tower reactor, a fixed bed reactor or a fluidized bed reactor. 7. Het micro-grensvlakversterkend reactiesysteem volgens claim 6, waarbij de micro- grensvlakgenerator is aangesloten op een inlaatuiteinde van het reactormanlichaam, en een aantal van de micro-grensvlakgenerator dat ten minste één 1s.7. The micro-interfacial enhancing reaction system of claim 6, wherein the micro-interfacial generator is connected to an inlet end of the reactor man body, and a plurality of the micro-interfacial generator is at least one 1s. 8. Het micro-grensvlakversterkend reactiesysteem volgens claim 1, waarbij een bereik van de micronorde groter is dan of gelijk is aan 1um en minder dan 1 mm. 208. The micro-interfacial strengthening reaction system according to claim 1, wherein a microorder range is greater than or equal to 1um and less than 1mm. 20