CN210385821U

CN210385821U - Ultrasonic intensified jet reactor

Info

Publication number: CN210385821U
Application number: CN201921101558.3U
Authority: CN
Inventors: 戚律; 王俊
Original assignee: Individual
Current assignee: Individual
Priority date: 2019-07-15
Filing date: 2019-07-15
Publication date: 2020-04-24
Anticipated expiration: 2029-07-15

Abstract

The utility model discloses an ultrasonic intensified jet reactor, wherein a plurality of groups of ultrasonic wave vibration generating devices are arranged on the outer wall of a reaction tube along the axial direction; the light phase liquid or the light phase gas entering through the light phase pipe and the heavy phase liquid entering through the heavy phase pipe are converged in the reaction pipe, intrinsic reaction is carried out under ultrasonic radiation, and the generated light phase reactant and the heavy phase reactant are discharged from a light phase outlet at the top and a heavy phase outlet at the bottom of the reaction pipe respectively through the aggregation separator. The gas or liquid is broken into small bubbles or liquid drops through ultrasound, and the small bubbles or liquid drops are uniformly dispersed in the medium-viscosity liquid in a short time, so that a large interphase contact area is provided, the mass transfer is enhanced, and the apparent reaction rate and the reaction selectivity are improved. The negative pressure formed by the jet flow combining component forms the flow force of the fluid in the reaction cavity; no additional power needs to be provided. The structure is simple, the interphase contact area is large, no stirring part is arranged, and the leakage is not easy to occur; can be widely used in the field of petrochemical industry, and has strong practicability and wide applicability.

Description

Ultrasonic intensified jet reactor

Technical Field

The utility model relates to a reactor, concretely relates to efflux formula reactor is reinforceed to supersound belongs to petrochemical, biochemical industry, environmental chemistry industry technical field.

Background

The mixing and dispersion of the two phases of insoluble gas-liquid and liquid-liquid has obvious influence on the mass transfer between the phases, namely the interphase area and the overall mass transfer coefficient. For fast reaction systems, such as benzene nitration and alkylation reactions, mass transfer between phases is a fast controlling step, and efficient mixing helps to promote mass transfer, thereby increasing reaction conversion and selectivity.

The mechanism of the mixing process comprises macro mixing and micro mixing, wherein the macro mixing mainly comprises the steps that a reactor drives a main phase fluid to make macro motion by means of energy input from the outside, meanwhile, turbulent flows with different sizes are formed to break a second phase fluid, bubbles or liquid drops with certain size distribution are formed, and the two phase fluid achieves uniform distribution on the equipment scale from the aspect of phase content rate. Micromixing refers to the uniform mixing on a molecular scale achieved by laminar diffusion between material micelles that are smaller in size than the smallest vortices. The gas-liquid and liquid-liquid mixing generally follows a macroscopic mixing mechanism, and usually utilizes moving parts and internal members arranged in a reactor to have strong interaction with the fluid to be mixed, so that the second-phase fluid forms bubbles or liquid drops, the breaking and coalescence balance is achieved, and a stable and uniform dispersion is formed.

In industrial production, reaction equipment for realizing gas-liquid and liquid-liquid two-phase mixing mainly comprises a stirring reaction kettle, a static mixer, a rotating packed bed and the like by utilizing the macroscopic mixing and turbulent dispersion effects.

In chemical production, the most common stirred tank reactor mainly comprises a tank body, an internal baffle, a stirring system, a transmission motor and a rotating shaft sealing device. Patent WO2014/118434 describes a gas-liquid stirred tank for enhancing gas dispersion, wherein a gas premixing cavity is arranged below a main paddle in the tank, a micro paddle coaxial (or coaxial) with the main paddle is arranged in the cavity, and gas is premixed and dispersed in the cavity and further dispersed by the main paddle during stirring to obtain more uniformly distributed small bubbles and enhance mass transfer. For a liquid-liquid reaction system with medium and high viscosity and a certain density difference between two phases, a horizontal stirring reactor is widely used at present, for example, patent ZL200520078557.3 discloses a horizontal reactor in a sulfuric acid alkylation process, and an internal circulation guide cylinder, a group of U-shaped tube bundles for removing reaction heat and an eccentrically-arranged turbine impeller are arranged in the horizontal reactor. The back mixing in the reactor is strong, and the reaction selectivity is easy to reduce. However, the mechanical rotating equipment is introduced into the stirring kettle, so that the sealing of the rotating bearing is difficult to ensure under the medium-pressure and high-pressure operating conditions.

Static mixers are a type of reaction apparatus that does not have mechanical rotation. When the two-phase fluid passes through the static mixer, the two-phase fluid is sheared into a liquid film by the built-in mixing element, and then the liquid film is stretched and broken into liquid drops, the number of the liquid drops is increased according to the power of the number of the elements, and the two-phase fluid is fully mixed after passing through a plurality of groups of elements. The static mixer has the advantages of large operation elasticity, compact structure, good sealing performance, low manufacturing cost, convenient installation and the like. However, if the reaction may produce solids, the static mixer tends to clog and is difficult to clean. In addition, static mixers have the disadvantage of a large pressure drop.

The rotary packed bed is a novel device for carrying out mixing reaction by using supergravity, and a two-phase fluid is sheared into a tiny liquid film, liquid silk or liquid drop through the rotary packed bed, so that a large two-phase contact area is created, and the mass transfer reaction effect is enhanced. ZL106929093 discloses a rotary packed bed reactor for alkylation of isobutane and C3-C5 olefin, which has a good dispersion effect of reaction raw materials and a liquid alkylation catalyst, can timely withdraw reaction heat and reduce catalyst consumption, but has the problems of dynamic sealing of the equipment under a high alkylation reaction pressure, and liquid drops on the side wall of the reactor are easy to generate and gather due to an overlarge centrifugal force.

SUMMERY OF THE UTILITY MODEL

In order to solve the defects of the prior art, the utility model aims to provide an ultrasonic intensified jet reactor which is suitable for gas-liquid and liquid-liquid multiphase reactions.

In order to achieve the above object, the utility model adopts the following technical scheme:

the ultrasonic intensified jet reactor is characterized in that a plurality of groups of ultrasonic wave vibration devices are arranged on the outer wall of a reaction tube along the axial direction;

the light phase liquid or the light phase gas entering through the light phase pipe and the heavy phase liquid entering through the heavy phase pipe are converged in the reaction pipe, intrinsic reaction is carried out under ultrasonic radiation, and the generated light phase reactant and the heavy phase reactant are discharged from a light phase outlet at the top and a heavy phase outlet at the bottom of the reaction pipe respectively through the aggregation separator.

The light phase outlet comprises a light phase gas outlet and a light phase liquid outlet;

the light phase gas outlet is arranged at the top of the reaction tube;

the light phase liquid outlet is arranged at the top side of the reaction tube, and an overflow weir matched with the light phase liquid outlet is arranged on the inner wall of the reaction tube.

The heavy phase tube is arranged at the bottom side of the reaction tube; the light phase pipe is a light phase nozzle and extends into the reaction pipe from the upper end or the lower end along the central axis of the reaction pipe;

if the reactor extends from the lower end, an upward spraying reactor is formed;

if the reactor extends from the upper end, a downward-spraying reactor is formed.

Furthermore, in the upward-spraying reactor, the reaction tube is provided with a throat, the light phase nozzle is positioned at one end of the throat, and the other end of the throat is provided with a reaction cavity;

in the lower spraying reactor, a flow guide pipe with the same central axis is arranged in a reaction cavity, an inner reaction cavity is arranged in the flow guide pipe, and an outer reaction cavity is arranged outside the flow guide pipe;

and the top of the flow guide pipe is provided with a horn-shaped flow collecting port, and the bottom of the flow guide pipe is provided with a pair of flow guide rings for guiding the flow to the outer reaction chamber.

Furthermore, in the upward-spraying reactor, the length of the throat is 1D-3D, the diameter of the throat is 0.4D-0.8D, wherein D is the inner diameter of the reaction cavity;

in the downward-spraying reactor, the diameter of the open end of the collecting port is 1.5d-3d, and the cone angle is 80-120 degrees; the diameter of the guide ring is d-1.5d, wherein d is the inner diameter of the guide pipe;

and the distance between the nozzle outlet and the section with the minimum diameter of the flow collecting port is less than the jet flow length of the nozzle.

Further, the light phase nozzle comprises an inlet pipe and a nozzle which are arranged at two ends of the buffer chamber;

the nozzles comprise a plurality of 2N auxiliary nozzles arranged around the main nozzle, and N is more than or equal to 1;

in the upward spraying reactor, the aperture ratio of the nozzle is 10-20% by taking the sectional area of the throat at the minimum diameter as a reference;

in the downward-spraying reactor, the opening rate of the nozzle is 15-25% based on the sectional area of the guide pipe.

The ultrasonic vibration generating device comprises a first ultrasonic vibration generating device and a second ultrasonic vibration generating device which are respectively arranged at the upper end and the lower end of the reaction cavity;

in the upward-spraying reactor, the distance between the first ultrasonic vibration generating device and the bottom end of the reaction cavity is 5D-8D, the frequency is 50-100kHz, the power is 600-; the distance between the second ultrasonic vibration device and the bottom end of the reaction cavity is 2D-4D, the frequency is 20-40kHz, the power is 200-500W, and the number is 2 m; m is 1,2, 3; d is the inner diameter of the reaction cavity;

in the lower-spraying reactor, the distance between the first ultrasonic vibration generating device and the open end of the flow collecting port is 3d-5d, the frequency is 100-150kHz, the power is 1000-1500W, and the quantity is 2 n; the distance between the second ultrasonic vibration generating device and the bottom end of the draft tube is 2d-4d, the frequency is 50-90kHz, the power is 200-900W, the number is 2n, and n is 2 and 3; d is the inner diameter of the flow guide pipe.

The ultrasonic wave vibration generator is fixed on the outer wall of the reaction tube through a connecting piece,

in the upward-spraying reactor, the distance between the end surface of an amplitude transformer of the ultrasonic oscillation generating device and the outer wall of the reaction tube is 0.5-1 cm;

in the downward-spraying reactor, the distance between the end surface of the amplitude transformer of the ultrasonic vibration generating device and the outer wall of the reaction tube is 0.2-0.5 cm.

The utility model discloses an useful part lies in:

the utility model discloses a jet flow formula reactor is reinforceed to supersound is applicable to the heterogeneous reaction of gas-liquid, liquid-liquid, is particularly useful for the heterogeneous reaction process that reaction mass viscosity middlely (10-100cp), the intersolubility is low (or not intersolubility). The gas or liquid is broken into small bubbles or liquid drops through ultrasound, and the small bubbles or liquid drops are uniformly dispersed in the medium-viscosity liquid in a short time, so that a large interphase contact area is provided, the mass transfer is enhanced, and the apparent reaction rate and the reaction selectivity are improved. The flow velocity of the jet flow is combined with the negative pressure formed by the member to form the flow force of the fluid in the reaction cavity; no additional power and power equipment need to be provided.

The multiphase reactor of the utility model has simple structure, large interphase contact area, no stirring part and difficult leakage; can be widely used in petrochemical field, especially in medium viscosity reaction system such as aromatic sulfonation, sulfuric acid alkylation, and alcohol amine CO absorption₂And the like, and has strong practicability and wide applicability.

Drawings

Fig. 1 is a schematic structural diagram of the upward-spraying reactor of the present invention.

Fig. 2 is a schematic structural diagram of the lower spray reactor of the present invention.

Fig. 3 is a schematic cross-sectional structure diagram of the light phase nozzle of the present invention.

Fig. 4 is a top view of the schematic structural diagram of the light phase nozzle of the present invention.

Fig. 5 is a schematic structural view of the ultrasonic vibration generator of the present invention.

Fig. 6 is a schematic structural view of the flow guide ring of the present invention.

Fig. 7 is a schematic view of an observation angle in embodiment 2 of the present invention (position B).

The designations in the drawings have the following meanings: 1. the device comprises a reaction pipe, 2, a throat pipe, 3, a light phase nozzle, 41, a first ultrasonic vibration device, 42, a second ultrasonic vibration device, 5, a gathering separator, 6, a light phase gas outlet, 7, an overflow weir, 8, a light phase liquid outlet, 9, a heavy phase outlet, 10, a heavy phase pipe, 11, a light phase pipe, 12, a settling chamber, 13, a phase separation chamber, 14, a flow guide pipe, 15, a flow collecting port, 16, a flow guide ring, 17, an outer reaction chamber, 18, a nozzle, 19, a buffer chamber, 20, a main nozzle, 21, an auxiliary nozzle, 22, a variable amplitude rod, 23, an ultrasonic transducer, 24 and an ultrasonic generator.

Detailed Description

The present invention will be described in detail with reference to the accompanying drawings and specific embodiments.

The utility model discloses the detecting instrument who uses does: on-line particle microscopy PVM815, by mettler-toledo, switzerland.

Example 1

The ultrasonically enhanced jet reactor shown in fig. 1 is an upward-injection reactor.

The main body of the upward-spraying reactor is a reaction tube 1, the lower waist part of the reaction tube 1 is in a throat pipe 2 shape, and the throat pipe 2 divides the inner cavity of the reaction tube 1 into a reaction cavity at the top end and a settling chamber 12 at the bottom end. The length of the throat 2 is 1D-3D, the diameter of the throat 2 is 0.4D-0.8D, wherein D is the inner diameter of the reaction cavity. The length of the reaction chamber is such that the residence time of the gas or liquid therein is not less than the intrinsic reaction time.

The light phase nozzle 3 (light phase pipe 11) extends from the lower end of the settling chamber 12 along the central axis of the reaction pipe 1 and is arranged at the bottom end of the throat pipe 2.

The light phase nozzle 3 consists of a nozzle 18 arranged at the top end of a buffer chamber 19 and an inlet pipe arranged at the bottom end of the buffer chamber 19; the nozzle 18 comprises a plurality of 2N auxiliary nozzles 21 arranged around the main nozzle 20, wherein N is more than or equal to 1; the aperture ratio of the nozzle 18 is 10 to 20% based on the sectional area of the throat 2 at the smallest diameter. The number of the sub-nozzles 21 is preferably 4.

And the distance between the outlet of the nozzle 18 and the minimum diameter section of the throat 2 is less than the jet length of the nozzle 18.

The heavy phase outlet 9 is arranged at the bottom edge of the settling chamber 12, and the aggregation separator 5 is arranged above the heavy phase outlet 9; the heavy phase pipe 10 is provided on the side wall of the settling chamber 12 symmetrical to the position of the aggregation separator 5.

The upper end of the reaction cavity is internally provided with a gathering separator 5, and the top end of the reaction cavity is divided into phase separation chambers 13; the light phase gas outlet 6 is arranged at the top of the phase separation chamber 13, the light phase liquid outlet 8 is arranged on the side wall of the phase separation chamber 13, and the overflow weir 7 matched with the light phase liquid outlet 8 is arranged on the inner wall of the phase separation chamber 13.

The components of the ultrasonic vibration generating device are mainly an ultrasonic generator 24, an ultrasonic transducer 23 and a variable amplitude rod 22; the small connecting piece is fixed on the outer wall of the reaction cavity by screws and adhesives (or only adhesives), and the distance between the end face of the amplitude transformer 22 connected with the connecting piece and the outer wall of the reaction tube 1 is 0.5-1 cm.

The first ultrasonic vibration generator 41 is arranged at the upper end of the outer wall of the reaction cavity, the distance between the first ultrasonic vibration generator and the bottom end of the reaction cavity is 5D-8D, the frequency of the first ultrasonic vibration generator is 50-100kHz, the power of the first ultrasonic vibration generator is 600-1000W, and the number of the first ultrasonic vibration generator is 2 m; the second ultrasonic vibration generator 42 is arranged at the lower end of the outer wall of the reaction chamber; the distance between the reaction chamber and the bottom end of the reaction chamber is 2D-4D, the frequency is 20-40kHz, the power is 200-500W, and the number is 2 m; m is 1,2, 3; d is the inner diameter of the reaction chamber.

In practice, the frequency, power and number of ultrasonic vibration generators may be suitably selected depending on the type and flow rate of the gas-liquid or liquid-liquid mixture to be dispersed and the desired degree of dispersion (average size of bubbles or droplets, uniformity of phase content).

The reaction process is as follows:

the heavy phase liquid is introduced from the lower side of the settling chamber 12, and the gas or light phase liquid is sprayed upwards into the throat 2 through the nozzle 18 of the light phase nozzle 3. Because the light phase object is sprayed into the throat 2 with the gradually reduced caliber, the generated negative pressure is combined with flowing air flow to link the heavy phase liquid to form fluid, and the fluid enters the reaction cavity through the throat 2.

After being fully mixed at the upper part of the throat pipe 2, the two flows enter the reaction cavity to continuously flow upwards for reaction, and keep a good dispersion state (the coalescence of bubbles or liquid drops is obviously inhibited and the distribution is uniform) under the ultrasonic radiation with different frequency intensities of the ultrasonic vibration device. The dispersion further rises to reach the top aggregation separator 5, and the gas-liquid or liquid-liquid two-phase rapid separation is realized.

For a gas-liquid reaction system, separated unreacted gas phase flows out from a light phase gas outlet 6 at the top, and a liquid product flows out from a light phase liquid outlet 8 over an overflow weir 7 and enters a subsequent operation unit; the heavy phase outlet 9 is closed all the time in the process.

For a liquid-liquid reaction system, after the liquid-liquid mixture is separated, a light-phase liquid product flows out from a light-phase liquid outlet 8 through an overflow weir 7 and enters a subsequent operation unit; while another part of the liquid-liquid mixture passes through the bottom aggregation separator 5 and is discharged from the heavy phase outlet 9.

Example 2

The ultrasonically enhanced jet reactor shown in fig. 2 is a down-jet reactor.

The main body of the downward-spraying reactor is a reaction tube 1, the bottom of the reaction tube 1 is a settling chamber 12, and the top of the reaction tube 1 is divided into a phase separation chamber 13 by a built-in aggregation separator 5; the light phase gas outlet 6 is arranged at the top of the phase separation chamber 13, the light phase liquid outlet 8 is arranged on the side wall of the phase separation chamber 13, and the overflow weir 7 matched with the light phase liquid outlet 8 is arranged on the inner wall of the phase separation chamber 13.

A heavy phase outlet 9 is arranged at the bottom end of the settling chamber 12 along the central axis of the reaction tube 1, and an aggregation separator 5 is arranged above the heavy phase outlet 9; if the dry weight phase pipe 10 is arranged in the side wall of the settling chamber 12.

The draft tube 14 and the reaction tube 1 are coaxially arranged in the reaction cavity, and the reaction cavity is divided into an inner reaction cavity in the draft tube 14 and an outer reaction cavity 17 outside the draft tube 14; and, the sum of the axial lengths of the inner and outer reaction chambers 17 should ensure that the residence time of the gas or light phase liquid therein is not less than the intrinsic reaction time.

The top of the draft tube 14 is provided with a trumpet-shaped collecting port 15, and the bottom is provided with a pair of draft rings 16 which guide the flow to an outer reaction chamber 17. The deflector ring 16 is two semicircular rings, and the tangential direction of the inner edge of the ring is parallel to the flow direction of the fluid at the outlet of the deflector tube 14, so that the fluid flows upwards after passing through the deflector ring 16. The diameter of the open end of the flow collecting port 15 is 1.5d-3d, and the cone angle is 80-120 degrees; the deflector ring 16 has a diameter d-1.5d, where d is the inner diameter of the draft tube 14.

The light phase nozzle 3 extends into the reaction tube 1 from the side wall of the phase separation chamber 13, is arranged along the central axis of the reaction tube 1, passes through the aggregation separator 5 and is opposite to the flow collecting port 15. The light phase nozzle 3 consists of a nozzle 18 arranged at the bottom end of a buffer chamber 19 and an inlet pipe arranged at the top end of the buffer chamber 19; the nozzle 18 comprises a plurality of 2N auxiliary nozzles 21 arranged around the main nozzle 20, wherein N is more than or equal to 1; the opening ratio of the nozzle 18 is 15 to 25% based on the sectional area of the draft tube 14. The number of the sub-nozzles 21 is preferably 4.

And the distance between the outlet of the nozzle 18 and the section with the smallest diameter of the collecting port 15 is smaller than the jet length of the nozzle 18.

The components of the ultrasonic vibration generating device are mainly an ultrasonic generator 24, an ultrasonic transducer 23 and a variable amplitude rod 22; the small connecting piece is fixed on the outer wall of the reaction cavity by screws and adhesives (or only adhesives), and the distance between the end face of the amplitude transformer 22 connected with the connecting piece and the outer wall of the reaction tube 1 is 0.2-0.5 cm.

The first ultrasonic vibration device 41 is arranged at the upper end of the outer wall of the reaction cavity, the distance between the first ultrasonic vibration device and the open end of the flow collecting port 15 is 3d-5d, the frequency is 100-1500 kHz, the power is 1000-1500W, and the number is 2 n; the second ultrasonic vibration generator 42 is arranged at the lower end of the outer wall of the reaction chamber; the distance between the bottom end of the draft tube 14 and the bottom end of the draft tube is 2d-4d, the frequency is 50-90kHz, the power is 200-900W, and the number is 2 n; n is 2, 3; d is the inner diameter of the draft tube 14.

The first ultrasonic vibration device 41 is slightly far from the open end of the manifold 15, so that larger ultrasonic energy is needed to maintain the desired dispersion state of the gas-liquid or liquid-liquid mixture in the outer reaction chamber 17; the second ultrasonic vibration means 42 is spaced slightly closer to the bottom end of the draft tube 14, and therefore requires less ultrasonic energy to maintain the desired dispersion of the gas-liquid or liquid-liquid mixture,

similarly, in practice, the frequency, power and number of ultrasonic vibration generators may be suitably selected depending on the type and flow rate of the gas-liquid or liquid-liquid mixture to be dispersed and the desired degree of dispersion (average size of bubbles or droplets, uniformity of phase content).

The reaction process is as follows:

heavy phase liquid is introduced from two sides of the lower part of the settling chamber 12, and gas or light phase liquid is sprayed downwards at high speed into the inlet of the lower draft tube 14 through the nozzle 18 of the light phase nozzle 3. Similarly, since the light phase is injected into the collecting port 15 with a gradually reduced diameter, the generated negative pressure is combined with the flowing air flow to form the power of the fluid.

After the two streams of fluid are premixed, the mixture continues to react and flow to the outlet in the draft tube 14, continues to perform a reaction approaching plug flow upwards after passing through the guide ring 16 along the tangential direction, and keeps a good dispersion state (the coalescence of bubbles or liquid drops is obviously inhibited and the distribution is uniform) under the ultrasonic radiation of the ultrasonic vibration device with different frequency intensities. When the reaction is nearly completed, the mixture contacts the aggregation separator 5 at the top, and the gas-liquid or liquid-liquid two-phase rapid separation is realized.

For a liquid-liquid reaction system, after the liquid-liquid mixture is separated, a light-phase liquid product flows out from a light-phase liquid outlet 8 through an overflow weir 7 and enters a subsequent operation unit; while another part of the liquid-liquid mixture, after passing through the bottom aggregation separator 5, is discharged from the heavy phase outlet 9.

The foregoing illustrates and describes the principles, general features, and advantages of the present invention. It should be understood by those skilled in the art that the above embodiments do not limit the present invention in any way, and all technical solutions obtained by adopting equivalent replacement or equivalent transformation fall within the protection scope of the present invention.

Claims

1. The ultrasonic intensified jet reactor is characterized in that a plurality of groups of ultrasonic wave vibration devices are arranged on the outer wall of a reaction tube along the axial direction;

2. The ultrasonically enhanced jet reactor of claim 1 wherein the light phase outlet comprises a light phase gas outlet and a light phase liquid outlet;

the light phase gas outlet is arranged at the top of the reaction tube;

3. The ultrasonically enhanced jet reactor according to claim 1, wherein the heavy phase tube is provided at a bottom side of the reaction tube; the light phase pipe is a light phase nozzle and extends into the reaction pipe from the upper end or the lower end along the central axis of the reaction pipe;

4. The ultrasonic-enhanced jet reactor according to claim 3, wherein in the upward-injection reactor, the reaction tube is provided with a throat, the light phase nozzle is positioned at one end of the throat, and the other end of the throat is a reaction cavity;

5. The ultrasonic-enhanced jet reactor according to claim 3, wherein in the upward-injection reactor, the throat has a length of 1D-3D and a diameter of 0.4D-0.8D, wherein D is the inner diameter of the reaction chamber;

6. The ultrasonic-enhanced jet reactor according to claim 3, wherein the light phase nozzle comprises an inlet pipe and a nozzle which are arranged at two ends of the buffer chamber;

7. The ultrasonic-enhanced jet reactor according to claim 1, wherein the ultrasonic vibration generator comprises a first ultrasonic vibration generator and a second ultrasonic vibration generator respectively disposed at the upper end and the lower end of the reaction chamber;

8. The ultrasonic-enhanced jet reactor according to claim 1, wherein the ultrasonic vibration generator is fixed to the outer wall of the reaction tube by a connecting member,