KR101690978B1

KR101690978B1 - Jet loop fludized bed reactor

Info

Publication number: KR101690978B1
Application number: KR1020150103750A
Authority: KR
Inventors: 이제근; 임준혁; 이태윤; 원용선
Original assignee: 부경대학교 산학협력단
Priority date: 2015-07-22
Filing date: 2015-07-22
Publication date: 2016-12-29

Abstract

The present invention relates to a jet loop reactor having improved gas-liquid absorption performance, comprising a reaction tank in which a gas-liquid absorption reaction is performed; A main body nozzle installed at an upper end of the reaction tank for mixing and spraying the main body in the direction of the lower end of the reaction tank; The upper and lower ends of which are opened to divide the space inside the reaction vessel into the space for descending the object and the space for raising the space for the object so that the object to be sprayed from the object nozzle can circulate within the reaction tank Induction tube to induce; A guide bottom plate installed at a lower end of the reaction tank and serving as a guide so as to guide the descended urine along the inside of the induction tube along the outside of the induction tube; And a fluidized bed installed in the elevated space of the reactor in the reaction tank divided by the induction pipe, the fluidized bed being filled with the fluidized bed.

Description

[0001] JET LOOP FLUDIZED BED REACTOR [0002]

More particularly, the present invention relates to a method and apparatus for enhancing mass transfer between phases in a heterogeneous phase reaction, and more particularly, The present invention relates to a jet loop fluidized bed reactor in which a fluid medium is disposed in a space between a reaction tank and a induction tube so as to improve mass transfer between the heterogeneous phases.

In chemical reactions, homogeneous reactions, which are reactions between the same substances, and heterogeneous reactions, which are reactions between different phases, can be divided. Such heterogeneous phase reactions include solid phase reactions such as gas-liquid reactions such as gas-liquid reactions such as coal gasification or iron ore reduction reactions, gas-solid reaction reactions such as liquid oxidation of hydrocarbons or reaction absorption of carbon dioxide, ion exchange reactions or immobilized enzyme reactions Liquid phase reaction which is a reaction between a liquid and a liquid and a liquid phase reaction which is a reaction between a liquid and a liquid which are not mixed with each other such as a sulfonation reaction or a polymerization reaction and a heterogeneous phase Catalytic reaction and the like.

In this heterogeneous phase reaction, phases involved in the reaction vary, and physical phenomena such as mass transfer overlap the chemical reaction and affect the apparent reaction rate. That is, at the overall apparent reaction rate, the mass transfer at the phase boundary rather than the actual chemical reaction rate corresponds to the main rate-determining step. Therefore, in such a nonuniform phase reaction, Mass transfer becomes a major issue, increasing the surface area of the interface for increased mass transfer rate, or increasing the turbulence of the reaction fluid.

Examples of the reactor for carrying out the above-described heterogeneous phase reaction include a packed tower reactor, an agitated vessel reactor, a bubble column reactor, a fluidized bed reactor, a jet loop reactor, -Loop Reactor).

The bubble column has a disadvantage in that the apparatus is simple and easy to manufacture but has a lower mass transfer efficiency than other apparatuses. The stirring reactor has a high turbulence intensity and a large contact area between the gas and the liquid by stirring the impeller, However, the apparatus for operating the impeller is complicated and has a disadvantage that it is difficult to scale-up for practical application on a suitable scale. The filling tower fills the device with the filling material and injects the liquid thereon, so that the device is simple and easily scaled up to a large capacity, but there is a disadvantage that the flow rate is limited in actual operation and the pressure drop is high.

The jet loop reactor requires a relatively low installation cost under high pressure conditions, and can reduce the size of gas compared to other reactors, increase the gas residence time due to internal circulation, thereby increasing the mass transfer between the heterogeneous phases, Has been attracting much attention because it is easy to control the heat of the reaction fluid by the heat of the reaction.

As shown in FIG. 1, the general structure of the jet loop reactor 10 includes an evaporator nozzle 12 including a first fluid inlet and a second fluid inlet, A circulation outlet 14 which is located at the upper end of the induction pipe 13 and the reaction tank 11 and in which a fluid mixture stream is circulated and discharged to form an external circulation flow, a circulation pump 15, And a discharge tube (16). The discharge pipe may be directly connected to the reaction tank, or branched from a line connected to the circulation outlet.

In such a structure, the jet loop reactor injects a heterogeneous phase such as gas and liquid at high speed using a nozzle, and the injected mixed fluid flows downward from the inside of the reaction vessel along the induction pipe, And moves upward to the space between the induction tubes. At this time, a negative pressure is generated due to a fluid mixing flow injected at a high pressure in the vicinity of the nozzle, and a flow near the induction pipe in the fluid mixing flow upward due to the negative pressure is sucked back into the induction tube, flow, and the internal circulation flow increases the residence time of the fluid mixture in the reactor, thereby increasing the amount of mass transfer between the non-uniform phases.

As a prior art for such a jet loop reactor, Korean Patent Registration No. 0484256 (Apr. 11, 2005) discloses a gas-liquid mixing apparatus using a jet loop reaction characteristic. The patent discloses a vapor- The present invention relates to a jet loop reactor for contacting and mixing a treatment water with a gas such as oxygen or ozone by the formation of annular flow through an injection tube and an induction tube, wherein a cone diffuser and a protrusion are formed in the induction tube, And the residence time in the treatment tank is increased, thereby improving the gas-liquid mixing performance.

Korean Patent No. 1403532 (Apr. 28, 2014) discloses a gas inflow pipe, a liquid inflow pipe which surrounds the gas inflow pipe and has a discharge port that is smaller than the inflow port, and a liquid inflow pipe which surrounds the outer wall of the gas inflow pipe and the inner wall of the liquid inflow pipe. A swirl flow generator and a weir guide member are installed in a reaction tank, and a weir swirl nozzle is installed instead of a conventional weir nozzle. Thus, The turbulence intensity is increased in the inside and the concentration gradient in the gas - liquid film is increased, so as to improve the gas - liquid mass transfer rate.

However, in such a conventional jet-loop reactor, there is a part where the liquid mixture flow of the liquid and gas injected into the reactor is internally circulated. However, in the mixing flow close to the reactor wall which is distant from the reactor nozzle, It was impossible to obtain the effect of increasing the residence time in the compartment, and when the gas-liquid mixture flow rises in the space between the induction pipe and the reactor wall, the phenomenon that the gas bubbles are bundled again can not be prevented.

The present invention solves the above-mentioned problems of the prior art and provides a novel jet loop reactor capable of enhancing gas-liquid mixing performance by improving the mass transfer phenomenon at the phase boundary in a mixed flow of gas and liquid, And the like.

More specifically, the present invention provides a fluidized bed in which a fluidized bed filled with a fluidizing medium is installed in a space where a fluid mixing flow rises to improve the non-uniform phase mixing performance of the jet loop reactor, , The gas bubble size in the fluid mixture flow is further subdivided and the fluid mixing flow forms turbulence by the fluidizing medium so that the mixing performance of the fluid as a whole can be greatly improved.

Further, according to the present invention, by providing a guide bottom plate for allowing the fluid mixing flow to move along the lower end of the reaction tank, the fluid mixing flow descended along the inner side of the induction pipe rises along the fluid mixing flow rising space located outside the induction pipe, The present invention provides a fluidized-bed reactor for a fluidized-bed reactor.

The jet loop fluidized bed reactor of the present invention comprises a reaction tank in which a heterogeneous reaction is performed; A nozzle located at a central axis of an upper end portion of the reaction tank and mixing and injecting a fluid into the reaction tank; An induction pipe installed in the reaction tank so as to divide the space inside the reaction tank into a space where the fluid mixture flow descends and a space where the fluid mixture flow rises; And a flow medium disposed in a rising space of the fluid mixing flow in the reaction vessel divided by the induction pipe.

Also, in one embodiment, the central axis of the induction pipe may be coaxial with the central axis of the reaction vessel.

In one embodiment, the nozzle may be located entirely or partially in the interior space of the induction tube, or may be located in a space above the induction tube. And a pump for sucking the fluid from the circulation outlet and transferring the fluid to the nozzle, wherein the circulation outlet is provided with a circulation outlet for circulating and discharging the fluid to form an external circulation flow, A filter may be present.

In one embodiment, the jet-loop fluidized-bed reactor is installed at the lower end of the reactor below the induction pipe, and the fluid mixing flow descended along the inside of the induction pipe is guided so as to rise along the space between the induction tube wall and the reactor wall And a guide deck that performs a role.

According to an embodiment of the present invention, the guide bottom plate is characterized in that the space between the center and the end of the bottom plate is concave downward.

In addition, in one embodiment, the fluidized medium is a solid material in particle form, sand, SiO _2, Al ₂ O _3, Fe ₃ O _4, FeO, a solid acid catalyst, supported or non-supported metal catalyst, immobilized enzyme Or a combination of at least one selected from these.

Further, in one embodiment, the rising space of the fluid mixing flow is provided with a screen at the lower end and / or the upper end of the rising space so that the flow medium fluidized by the upwardly moving fluid mixing flow stays in the rising space .

In one embodiment, the reaction tank is characterized in that at least a part of the slanted part, which is perpendicular to the direction of fluid flow, is widened from the lower part to the upper part.

The present invention relates to a jet loop fluidized bed reactor in which fluid mixing performance is improved and a fluid mixture stream such as a gas and a liquid which is strongly jetted from the nozzle is jetted out of the nozzle along the outer side of the draft tube, By moving the loop moving gas and liquid through the fluidized bed filled with the fluid medium, the size of the dispersed fluid (for example, the gas bubbles dispersed in the liquid) dispersed in the fluid mixed in the reactor is reduced and the residence time is increased The turbulence intensity is increased and the vapor-liquid mixing performance can be improved.

1 is a view for explaining a general jet loop reactor.
FIG. 2 illustrates a jet loop fluidized bed reactor according to an embodiment of the present invention.
3 is a view for explaining a jet loop fluidized bed reactor equipped with a guide bottom plate according to an embodiment of the present invention.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, preferred embodiments of a jet loop fluidized bed reactor having improved mixing performance between heterogeneous phases according to the present invention will be described in detail so that those skilled in the art can easily carry out the present invention.

In the present invention, the term " heterogeneous phase reaction "refers to a reaction in which two or more phases participate in a reaction, and a reaction between different phase materials; Dissolving the gas in a liquid or solid; Degassing of the gas from the solid or liquid, and the like. The two or more phases include liquid-liquid phases which are not formed in a single phase with each other.

In the drawings of the present invention, the sizes and dimensions of the structures are enlarged or reduced from the actual size in order to clarify the present invention, and the known structures are omitted so as to reveal the characteristic features, and the present invention is not limited to the drawings .

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings. In the following description, well-known functions or constructions are not described in detail to avoid obscuring the subject matter of the present invention.

In addition, since the embodiments described in the present specification and the configurations shown in the drawings are only the most preferred embodiments of the present invention and do not represent all the technical ideas of the present invention, It is to be understood that equivalents and modifications are possible.

The present invention relates to an apparatus for mixing and reacting a mixed fluid flow in a heterogeneous phase, for example, a gas and a liquid, using a nozzle for mixing and injecting a fluid and an induction tube, wherein a fluidized bed filled with a fluid medium is provided in the reaction tank, Wherein the fluidized bed is passed through the loop to increase the intermixture rate of the fluid mixture stream and the mass transfer coefficient between the non-homogeneous fluid, wherein the heterogeneous reaction is performed; A nozzle located at a central axis of an upper end portion of the reaction tank and mixing and injecting a fluid into the reaction tank; An induction pipe installed in the reaction tank so as to divide the space inside the reaction tank into a space where the fluid mixture flow descends and a space where the fluid mixture flow rises; And a flow medium disposed in a rising space of the fluid mixing flow in the reaction vessel divided by the induction pipe.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, the present invention will be described in detail with reference to the accompanying drawings.

1 shows a jet loop reactor according to the prior art of the present invention. The first fluid and the second fluid are simultaneously injected from the sieve nozzle 12 and discharged into the jet stream, so that the first fluid and the second fluid are mixed with each other. The mixed flow of the rejected substance discharged from the evaporator nozzle 12 is discharged to the jet stream inside the induction pipe 13 and descends to the lower end of the reactor along the induction pipe. The mixed flow of the reactant reaching the bottom of the reactor collides with the bottom surface and then turns again to raise the space between the wall of the induction pipe 13 and the wall of the reactor 11, The upward flow of the mixed fluid of the lean body which is in the vicinity of the induction pipe 13 is sucked into the induction pipe 13 due to the negative pressure generated when the jet flow is discharged from the lean nozzle 12. In addition, a circulation outlet 14 for forming an external circulation flow is provided at the upper end of the reaction tank, and the fluid in the reaction tank is further transferred to the nozzle by the circulation pump 15 connected to the circulation outlet to form an external circulation flow . And a discharge pipe 16 for removing the fluid treated in the reaction tank from the reaction vessel.

FIG. 2 illustrates a jet loop fluidized bed reactor according to an embodiment of the present invention. As shown therein, the jet loop fluidized bed reactor of the present invention includes a reactor 110, an induction nozzle 120, A tube 130 and a fluidized bed 140.

An injection nozzle 120 for injecting two or more fluids in different phases toward a lower end of the reaction tank 110 is provided at an upper end of the reaction tank 110. Each of the nozzles 120 has a fluid injection unit, For example, when the fluid has two phases, the first fluid and the second fluid injecting portion are formed in a concentric cylindrical shape, and different fluids are supplied to the inside and the outside, and mixed and injected.

The induction pipe 130 is installed at the lower end of the nozzle 120 to open both ends in the vertical direction. The inside of the reaction tank 110 is connected to the fluid mixing flow- It is divided into rising space.

The fluidized bed (140) disposed between the induction tube wall and the reactor wall has a structure including a fluid medium. The fluidized bed is divided into a fluid rising space inside the reaction tank (110) divided by the induction tube And the flow medium is fluidized by the upward flow of the fluid mixture.

On the other hand, the fluidized medium may be sand which is generally used as a fluidized medium, and various kinds of catalysts may be used in the form of particles according to a reaction to be performed. Particles used in the catalyst, _{SiO 2, Al 2 O 3,} Fe 3 O 4, FeO, zeolite, a metal catalyst, but include one or more combinations may be used which is selected from the enzymes and their immobilization on particles, limited to And includes all of the materials that can be used as the flow medium.

In addition to the above-described configuration, a configuration such as a discharge port for discharging the solidified reaction product in the reaction tank 110 or a discharge pipe for discharging the treated liquid and gas or the like is generally used in a jet loop reactor, And therefore the detailed description will be omitted.

The operation principle of the jet loop fluidized bed reactor of the present invention is as follows.

The fluid mixing flow is injected into the reaction tank 110 at a high speed through the nozzle 120 through which the fluid of different phases is injected and mixed and injected. 130 to the lower part of the reaction tank 110 and then to the upper part of the reaction tank 110 along the outer side of the induction pipe 130 to pass through the fluidized bed 140. [ For example, if the mixed fluid is a gas and a liquid, the fluid mixing stream rising above the reaction tank 110 collides with the fluid medium in the fluidized bed 140 while passing through the fluidized bed 140, The generated bubble size is further finely divided and the fluid mixing flow impinging on the fluid medium is scattered in the direction of the turbulence to increase the turbulence intensity to increase the gas mixture ratio and to increase the turbulence intensity in the fluid mixing flow The mass transfer rate is improved.

Or when the fluidized bed is a catalyst, it is possible to increase the contact rate with the catalyst to improve the reaction rate, and to allow the reaction to proceed evenly in a relatively large space, so that the reaction heat that can be generated during the reaction can be easily controlled.

The fluid mixture flow that has passed through the fluidized bed 140 flows upward to the upper part of the reaction vessel 110 and then flows into the induction pipe 130 through the fluid mixing flow and then sucked into the induction pipe 130 by differential pressure to form a ring flow in the reaction tank 110.

In contrast to the prior art, the jet loop fluidized bed reactor of the present invention places the flow medium in a space where the fluid mixture flow rises, increasing the turbulence intensity of the fluid mixture flow due to the effect of the flow medium, This has the advantage of making the fluid more finer.

In the jet-loop fluidized-bed reactor, the shape of the reactor may be such that at least a part of the slanted part 111 is formed such that the cross-sectional area of the reactor perpendicular to the fluid flow direction becomes wider from the lower part toward the upper part. When the inclined portion 111 is present, the linear velocity at the time of ascending of the fluid mixture flow decreases gradually toward the inclined portion, so that the flow medium can be adjusted so as not to overflow in the space of the fluidized bed 140 .

At this time, in the fluidized bed, the fluidized bed may be formed without adjusting the rising velocity of the fluid mixture flow and the density of the fluidized medium so that the fluidized bed can not escape from the fluidized bed space. However, A screen may be provided on each of the lower and upper portions of the space to be disposed so that the flow medium stays in the rising space.

In the jet flow fluidized bed reactor in which the fluid medium is arranged as described above, the inlet and the outlet may be installed so that the fluid medium can be introduced into or discharged from the upper space and the lower space of the space in which the fluid medium is disposed. It is to be understood that the present invention may be embodied in many other specific forms without departing from the spirit or essential characteristics of the invention.

At the top of the reactor is a circulation outlet 160 for discharging the fluid mixing flow in the reactor to the outside to form an external circulation flow to form an external circulation flow of the fluid mixing flow. At this time, there may be a filter for filtering the solid phase material such as the flowing medium, which may be introduced in the circulation outlet 160 or the outer circulation line 170 at one portion.

3 is a view for explaining a jet loop reactor provided with a guide bottom plate according to an embodiment of the present invention.

In the conventional jet loop reactor, the fluid mixture is not circulated at the lower end of the reaction tank 11 and a dead volume is generated, thereby preventing the fluid mixing stream from effectively forming the annular flow. As a result, the overall non- . In addition, when the fluidized medium is disposed between the induction tube wall and the reactor wall as in the present invention, the flow medium is trapped within the congestion region due to a dead volume inevitably generated.

3, the bottom of the reaction vessel 110 is lowered along the inner side of the induction pipe 130 at the lower end of the reaction vessel 110 and is naturally stagnated at the lower end of the reaction vessel 110, And a guide bottom plate 150 serving as a guiding guide.

That is, the guide bottom plate 150 is installed at the lower end of the reaction tank 110 to prevent the bottom of the reaction tank 110 from being stagnated without being circulated to the reaction tank 110 by the sieve discharged from the sieve nozzle 120, So that the weft body reaching the lower end can smoothly move to the weft body elevating space outside the weft body flow guide portion. It is preferable that the guide bottom plate 150 has a structure in which a space between the center 151 and the distal end 152 of the guide bottom plate is concave downward.

Due to the above structure, the descending body along the inner side of the induction pipe 130 can move to the elevated body elevating space along the surface of the bottom plate without a large resistance.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is clearly understood that the same is by way of illustration and example only and is not to be taken by way of limitation, I will understand. Accordingly, the technical scope of the present invention should be defined by the following claims.

10: (conventional) jet loop reactor
11: (Conventional) Reactor
12: (Conventional) Ignition nozzle
13: (Conventional) induction tube
14: (Conventional) circulation outlet
15: (Conventional) circulation pump
16: (conventional) discharge pipe
17: (conventional) second circulation outlet
100: jet loop reactor
110: Reactor
120: Ignition nozzle
130: Induction tube
140: Fluidized bed
150: guide bottom plate
151: center of guide bottom plate
152: End of guide bottom plate
160: Circulating outlet
170: External circulation line
171: Outlet
180: circulation pump
190: 2nd circulation outlet
191: Second discharge pipe

Claims

A reaction tank in which a heterogeneous reaction is performed;
A nozzle located at a central axis of an upper end portion of the reaction tank and mixing and injecting a fluid into the reaction tank;
An induction pipe installed in the reaction tank so as to divide the space inside the reaction tank into a space where the fluid mixture flow descends and a space where the fluid mixture flow rises;
And a fluid medium disposed in a rising space of the fluid mixing flow in the reactor divided by the induction tube and fluidized by the upward flow of the fluid mixing flow.

The method according to claim 1,
Wherein the central axis of the induction pipe is located coaxially with the central axis of the reaction vessel.

The method according to claim 1,
Wherein the nozzle is located entirely or partially in the interior space of the induction tube or in a space above the induction tube.

The method according to claim 1,
Further comprising a circulation outlet for circulating the fluid in the upper end wall of the reaction tank, and a pump for sucking the fluid from the installed circulation outlet and transferring the fluid to the nozzle.

The method of claim 4,
Wherein the circulation outlet is provided with a filter for filtering solid matter.

The method according to claim 1,
And a guide bottom plate installed at a lower end of the reaction tank below the induction pipe and serving as a guide so as to guide the fluid mixing flow descended along the inside of the induction pipe upward along a space between the induction pipe wall and the reaction tank wall Wherein the fluidized bed reactor comprises a plurality of fluidized bed reactors.

The method of claim 6,
Wherein the guide bottom plate has a concave downward space between the center and the end.

The method according to claim 1,
The fluidized medium is a solid material in particle form, sand, SiO _2, Al ₂ O _3, Fe ₃ O _4, FeO, a solid acid catalyst, supported or supported one that is not is selected from a metal catalyst, immobilized enzyme or both are And a combination of the above.

The method according to claim 1,
Characterized in that in the rising space of the fluid mixing flow a screen is installed at the lower end and / or the upper end of the rising space so that the flow medium fluidized by the ascending moving fluid mixing flow stays in the rising space. .

The method according to claim 1,
Wherein the reaction tank has at least a part of a slanted part that is wider in cross section perpendicular to the fluid flow direction from the lower part to the upper part.