KR20200005876A - Circulation heat exchange type of catalyst regenerator and regeneration method thereof - Google Patents

Abstract

Provided by an embodiment of the present invention is a catalyst regenerator of a circulating heat exchange method, which originally prevents a coking catalyst, a regeneration target, from being exposed to an environment of a high temperature. According to an embodiment of the present invention, the catalyst regenerator of a circulating heat exchange method includes: a medium supply unit which supplies a heat transfer medium; a medium heating unit which heats a heat transfer medium supplied from the medium supply unit by a first combustion action; a mixing/heat exchanging unit which mixes the heat transfer medium heated by being supplied from the medium heating unit and the coking catalyst supplied after a previous process, and exchanges heat with each other; a separation unit which mutually separates the mixed coking catalyst and heat transfer medium supplied from the mixing/heat exchanging unit; and a catalyst regenerating unit which regenerates the coking catalyst supplied from the separation unit by combusting remaining cokes with a second combustion action.

Description

Circulation heat exchange type catalyst regenerator and its regeneration method {CIRCULATION HEAT EXCHANGE TYPE OF CATALYST REGENERATOR AND REGENERATION METHOD THEREOF}

The present invention relates to a cyclic heat exchange type catalyst regenerator and a regeneration method thereof, and more particularly, to a cyclic heat exchange type catalyst regenerator and a regeneration method of preventing a coking catalyst, which is a regeneration target, from being exposed to a high temperature environment.

In general, ethylene is a representative material of basic raw materials in petrochemicals. The petrochemical process produces various substances through various processes based on olefin compounds such as ethylene and propylene.

Catalysts are used to produce olefins from naphtha. The catalyst is coked in the course of naphtha cracking. That is, carbon particles cover the surface of the catalyst.

The coking catalyst covered with carbon is recycled and then mixed with naphtha to undergo a cycle used for the decomposition reaction of naphtha. By the way, when the catalyst is coked, it becomes difficult for the naphtha decomposition reaction to occur smoothly.

As disclosed in US Pat. No. 7,153,479, when regenerating the coking catalyst, the fuel supplying method uses a nozzle to inject liquid fuel into the catalyst fluidized bed in powder form.

As such, the method of injecting liquid fuel may generate a hot spot where heat is concentrated in the catalyst fluidized bed due to the low dispersion performance of the fuel. The generation of hot spots will expose the coking catalyst to be regenerated at high temperatures.

After the catalyst is exposed to high temperature, the performance of the catalyst is reduced. Therefore, the replacement cycle of the catalyst is shortened. This increases the process cost in the olefin production process.

One embodiment of the present invention relates to a cyclic heat exchange type catalyst regenerator which prevents the coking catalyst, which is a regeneration target, from being exposed to a high temperature environment. In addition, an embodiment of the present invention relates to a cyclic heat exchange catalyst regeneration method for regenerating the coking catalyst using the cyclic heat exchange catalyst regenerator.

According to one embodiment of the present invention, a circulating heat exchange type catalyst regenerator includes a medium supply unit for supplying a heat transfer medium, a medium heating unit for heating the heat transfer medium supplied from the medium supply unit in a first combustion operation, and supplying from the medium heating unit. A mixing / heat exchange unit for mixing the heated heat transfer medium and the coking catalyst supplied after the previous process to heat exchange with each other, a separation unit separating the mixed coking catalyst and the heat transfer medium supplied from the mixing / heat exchange unit, and the separation unit And a catalyst regeneration unit for regenerating the coking catalyst supplied from the second combustion by burning residual coke.

The heat transfer medium has a specific gravity greater than that of the catalyst and may be formed of alumina balls or metal balls having a large heat capacity.

The previous process is a olefin production process of the fluid catalyst cracking (FCC) method, the first combustion unit may use methane generated as a by-product in the process.

The medium heating part includes a first chamber forming a first combustion space, a medium inflow pipe connected to the medium supply part and extending inside the first chamber to introduce the heat transfer medium, and a high temperature heated in the first combustion space. It may include a heating medium pipe for supplying a heat transfer medium of the mixing / heat exchange unit.

The medium heating unit may further include a first air supply line and a first fuel supply line for supplying air and fuel to the first combustion space, respectively, for the first combustion operation.

The mixing / heat exchange part includes a mixing / heat exchange chamber that forms a mixing / heat exchange space, and a caulking catalyst conduit connected to an upper portion of the mixing / heat exchange chamber to supply a caulking catalyst from a stripper, wherein the high temperature heat transfer is performed from the first chamber. A heating medium conduit for supplying a medium may be connected to the coking catalyst conduit, and the mixing / heat exchange chamber may be connected to the separation unit via a mixing conduit for supplying a heated caulking catalyst mixed with a high temperature heat transfer medium.

The separation unit separates the heated coking catalyst and the cooled heat transfer medium which are connected to the mixing / heat exchange chamber and is supplied to the mixing / heat exchange chamber by a mixing conduit, and is extended to the upper side to supply the separated and heated coking catalyst to the catalyst regeneration unit. And a recovery conduit connected to the lower side of the separation / heat coking catalyst conduit to recover the separated and cooled heat transfer medium to the medium supply.

The catalyst regeneration unit includes: a second chamber forming a second combustion space, a caulking catalyst inlet conduit extending inside the second chamber to introduce a separated and heated coking catalyst connected to the separation unit, and the second combustion space It may include a regeneration catalyst pipeline for supplying the regenerated catalyst to the previous process by burning the residual coke at the.

The catalyst regeneration unit may further include a second air supply line and a second fuel supply line for supplying air and fuel to the second combustion space, respectively, for the second combustion operation.

The catalyst regenerator and the regeneration method of the circulating heat exchange method according to an embodiment of the present invention, the medium supply step of supplying a heat transfer medium, the medium heating step of heating the heat transfer medium supplied from the medium supply step, from the medium heating step A mixing / heat exchange step of mixing the heated heat transfer medium supplied with the coking catalyst supplied after the preceding process and exchanging heat with each other, a separation step of separating the mixed coking catalyst and the heat transfer medium supplied from the mixing / heat exchange step from each other, and the separation A catalyst regeneration step of burning and regenerating residual coke in the heated coking catalyst supplied from the step.

The medium heating step includes the step of introducing the heat transfer medium into a first combustion space, heating the heat transfer medium to a high temperature in the first combustion space supplied with fuel and air, and mixing the heated high temperature heat transfer medium It may include the step of supplying / heat exchange step.

The mixing / heat exchange step includes introducing a coking catalyst into a mixing / heat exchange chamber in a stripper, introducing a high temperature heat transfer medium heated in the medium heating step into the mixing / heat exchange chamber, and introducing the coking catalyst and the high temperature heat transfer. Mixing / heat exchanging the medium in the mixing / heat exchange chamber, and feeding the coking catalyst heated by mixing with the high temperature heat transfer medium together with the cooled heat transfer medium to the separation step.

The separating step is a step of separating the heated caulking catalyst and the cooled heat transfer medium introduced in the mixing / heat exchange step in a separation / heating coking catalyst pipeline and supplying the separated heated caulking catalyst to the catalyst regeneration step, and the separation Recovering the cooled heat transfer medium separated from the heated coking catalyst duct to the medium feed stage.

The catalyst regeneration step may include introducing a heated coking catalyst into a second combustion space, regenerating by regenerating residual coke from the coking catalyst heated in the second combustion space supplied with fuel and air, and regenerating the regenerated catalyst. It may include the step of supplying to the previous process.

In one embodiment of the present invention, the heat transfer medium supplied is heated by a first combustion action, mixed with a coking catalyst to exchange heat with each other, and then the mixed caulking catalyst and the heat transfer medium are separated from each other, and separated heating by a second combustion action. Since the catalyst is regenerated by burning the residual coke of the coking catalyst, the regenerated catalyst can be fed to the previous process.

At this time, since the coking catalyst is indirectly heated by the heat transfer medium and heat transfer heated by the first combustion action, the coke catalyst is regenerated by burning residual coke, and thus, the coking catalyst to be regenerated may be prevented from being exposed to a high temperature environment.

That is, one embodiment heats the heat transfer medium in the medium heating unit (first combustion), and mixes and heats the coking catalyst in the mixing / heat exchange unit to heat the coking catalyst, thereby enabling the use of gaseous fuel in catalyst regeneration. Exposure of the catalyst to high temperature environments can be prevented.

As such, since the medium heating unit burns gaseous fuel, it is possible to fundamentally prevent after-burning generated in the conventional catalyst regenerator. The heated heat transfer medium can prevent the occurrence of hot spots during the mixing and heat transfer process.

In addition, one embodiment includes a catalyst regeneration unit (second combustion operation) to burn and remove the coke remaining in the coking catalyst, so that the coking catalyst can be effectively regenerated. Therefore, after regeneration, the performance of the catalyst is not deteriorated, and the replacement cycle of the catalyst can be maintained without being shortened. In other words, an increase in process cost can be prevented.

1 is a block diagram of a catalyst regenerator of the circulation heat exchange method according to an embodiment of the present invention.
FIG. 2 is a detailed view of the medium heating part of FIG. 1.
3 is a detailed view of the heat exchange / mixing unit of FIG. 1.
4 is a detailed view of the separator of FIG. 1.
5 is a detailed view of the catalyst regeneration unit of FIG. 1.
6 is a flowchart of a catalyst regeneration method of a circulating heat exchange method according to an embodiment of the present invention.

Hereinafter, exemplary embodiments of the present invention will be described in detail with reference to the accompanying drawings so that those skilled in the art may easily implement the present invention. As those skilled in the art would realize, the described embodiments may be modified in various different ways, all without departing from the spirit or scope of the present invention. In the drawings, parts irrelevant to the description are omitted in order to clearly describe the present invention, and like reference numerals designate like elements throughout the specification.

1 is a block diagram of a catalyst regenerator of the circulation heat exchange method according to an embodiment of the present invention. Referring to FIG. 1, the cyclic heat exchange type catalyst regenerator heat transfer mixes and heats the coking catalyst used in the previous process to the solid state heat transfer medium (M) while heating and circulating the heat transfer medium (M), and the coking catalyst. And to regenerate the catalyst by burning the coke remaining in the.

Although not shown, the fluidized bed reactor mixes the reactants and the catalyst (or regenerated catalyst) in a riser (not shown) to cause a decomposition reaction of the reactants, and then separates the caulked coking catalyst and the product into a cyclone to separate the caulking catalyst. Is dropped into the catalyst regenerator of the circulating heat exchange method.

In one embodiment, a process of producing olefins using naphtha as a reactant, that is, a process of producing an olefin by a fluid catalyst cracking (FCC) method, corresponds to the previous process of this embodiment, and may be used as fuel as a by-product of methane. Generates.

The previous process mixes naphtha and catalyst, causes naphtha decomposition reaction, separates the caulked catalyst and the produced olefin from a cyclone (not shown), and drops the coking catalyst into a cyclic heat exchange catalyst regenerator.

That is, naphtha is injected into the bottom of the riser and encounters a high temperature catalyst (including a regenerated catalyst) and begins to decompose through a catalytic reaction. Naphtha continues to endothermally decompose as it rises along the riser.

After the naphtha decomposition reaction, the catalyst covered with solid carbon particles, that is, the coking catalyst and the olefin produced in the decomposition reaction, enter the cyclone and are separated from each other. The caulking catalyst separated from the cyclone falls into the catalyst regenerator of the circulation heat exchange method. That is, the catalyst of the preceding process is dropped into the stripper 33 and supplied to the catalyst regenerator of the circulation heat exchange method.

The cyclic heat exchanger catalyst regenerator of one embodiment is configured to regenerate the coking catalyst used in the previous process while heating and circulating the heat transfer medium (M). That is, one embodiment includes a medium supply unit 10, a medium heating unit 20, a mixing / heat exchange unit 30, a separation unit 40, and a catalyst regeneration unit 50.

The medium supply unit 10 is configured to supply the solid state heat transfer medium M. That is, the medium supply unit 10 supplies the heat transfer medium M to the medium heating unit 20 while supplying a moving fluid. As an example, the heat transfer medium M may have a specific gravity greater than that of the powdered caulking catalyst, and may be formed of alumina balls or metal balls having solid sand or large heat capacity.

Therefore, the heat transfer medium M may absorb heat in the medium heating unit 20 and then be mixed with the coking catalyst used in the previous process to implement heat exchange to supply heat to the coking catalyst by heat transfer. At this time, the caulking catalyst is not directly exposed to high heat, it may be indirectly heated by the heat transfer medium (M).

FIG. 2 is a detailed view of the medium heating part of FIG. 1. 1 and 2, the medium heating unit 20 is configured to first heat the heat transfer medium M supplied with the moving fluid from the medium supply unit 10.

For example, the medium heating unit 20 includes a first chamber 21, a medium inlet conduit 22, and a heating medium conduit 23. The first chamber 21 forms a first combustion space BS1 for heating the solid state heat transfer medium M. FIG.

The medium inlet conduit 22 is connected to the medium supply unit 10 and extends inside the first chamber 21 to introduce the heat transfer medium M together with the moving fluid. That is, the medium inlet conduit 22 extends further inside the first chamber 21 while connecting the medium supply part 10 and the first chamber 21 so that one end thereof is exposed and opened in the first chamber 21. do. As an example, the medium inlet conduit 22 may be vertically installed and connected to the upper first chamber 21.

The heating medium conduit 23 is connected to the mixing / heat exchange unit 30 to supply the high temperature heat transfer medium M heated in the first combustion space BS1 to the mixing / heat exchange unit 30. That is, the heating medium pipe 23 connects the medium heating part 20 and the mixing / heat exchange part 30.

On the other hand, the medium heating unit 20 and the first air supply pipe 24 for supplying air and fuel to the first combustion space (BS1), respectively, in order to heat the solid-state heat transfer medium (M) by the first combustion action; It further comprises a first fuel supply line (25).

The first air supply line 24 and the first fuel supply line 25 supply air and fuel from the outside, and burn the heat transfer medium M by burning in the first combustion space BS1 of the first chamber 21. ) Can be heated. At this time, when using methane (CH ₄ ) generated as a by-product in the previous process for producing olefins as a fuel, the process cost can be reduced.

The first air supply line 24 and the first fuel supply line 25 are formed in a donut shape disposed outside the medium inlet line 22 inside the first chamber 21, and the air is provided by a plurality of nozzles. And the fuel are uniformly injected to enable a uniform first combustion action in the first combustion space BS1.

In addition, the medium heating unit 20 introduces the moving fluid and the heat transfer medium M supplied to the first chamber 21 into the cyclone 26 installed therein, and separates the moving fluid and the heat transfer medium M. .

The separated moving fluid is discharged out of the first chamber 21, the heat transfer medium M is heated while passing through the first chamber 21, and supplied to the mixing / heat exchange unit 30 through the heating medium conduit 23. do. As an example, the heating medium pipe 23 may be inclined to connect the upper first chamber 21 to the lower mixing / heat exchange part 30.

As such, the medium heating unit 20 heats the solid-state heat transfer medium M by the first combustion action to heat the coking catalyst, so that gaseous fuel may be used to regenerate the coking catalyst. May not be directly exposed to high temperature environments.

3 is a detailed view of the heat exchange / mixing unit of FIG. 1. 1 and 3, the mixing / heat exchange unit 30 is configured to mix the heated heat transfer medium M supplied from the medium heating unit 20 and the caulking catalyst supplied after the previous process, and to heat exchange with each other. do.

For example, the mixing / heat exchange unit 30 includes a mixing / heat exchange chamber 31 and a caulking catalyst conduit 32. The mixing / heat exchange chamber 31 forms a mixing / heat exchange space (MHS) in which the heated heat transfer medium (M) and the coking catalyst are mixed to exchange heat with each other.

The caulking catalyst conduit 32 is connected above the mixing / heat exchange chamber 31 to supply (ie, drop) the caulking catalyst supplied to the stripper 33 in the preceding process to the mixing / heat exchange chamber 31.

The heating medium conduit 23 connects the first chamber 21 and the caulking catalyst conduit 32 to each other, and mixes a high temperature heat transfer medium M from the first chamber 21 via the caulking catalyst conduit 32. / To the heat exchange chamber (31).

Therefore, the high temperature heat transfer medium (M) and the coking catalyst in the caulking catalyst conduit 32 are mixed with each other to exchange heat. The mixing / heat exchange chamber 31 further mixes and heat-exchanges the high temperature heat transfer medium M and the coking catalyst in the mixing / heat exchange space MHS.

And the mixing / heat exchange chamber 31 is connected to the separator 40 by a mixing conduit 34. Therefore, the coking catalyst heated by mixing with the high temperature heat transfer medium M in the mixing / heat exchange chamber MHS of the mixing / heat exchange chamber 31 is supplied to the separation unit 40 through the mixing conduit 34. As an example, the mixing conduit 34 may be inclined to connect the upper mixing / heat exchange chamber 31 to the lower separating part 40.

At this time, the caulking catalyst is heated within the temperature range of the heated heat transfer medium (M) and thus is not exposed to high temperatures. And the heat transfer medium (M) is maintained in a relatively cooled state when supplied to the mixing conduit 34, compared to when supplied to the heating medium conduit (23).

4 is a detailed view of the separator of FIG. 1. 1 and 4, the separator 40 is configured to separate the mixed caulking catalyst and heat transfer medium M supplied from the mixing / heat exchange unit 30 from each other. That is, by the heat exchange action, the caulking catalyst is heated to a high temperature, and the heat transfer medium M is cooled to a low temperature.

For example, the separator 40 includes a separation / heating caulking catalyst conduit 41 and a recovery conduit 42. Separation / heating caulking catalyst conduit 41 makes it possible to separate the high temperature caulking catalyst and the low temperature heat transfer medium (M) by the difference in specific gravity according to gravity. As an example, the separation / heating caulking catalyst conduit 41 is installed vertically.

To this end, a moving fluid is supplied to the lower end of the separation / heating caulking catalyst conduit 41. That is, the separation unit 40 may separate the coking catalyst from the heat transfer medium M by the difference in gravity and drag according to the flow rate of the coking catalyst and the heat transfer medium M corresponding to the moving fluid.

Separation / heating caulking catalyst conduit 41 is connected to mixing / heat exchange chamber 31 by mixing conduit 34 to separate the heated caulking catalyst and cooled heat transfer medium M fed to mixing conduit 34. It is composed.

The separation / heating caulking catalyst conduit 41 is extended upward and separated by a moving fluid to supply a heated caulking catalyst to the catalyst regeneration unit 50.

The recovery conduit 42 is connected to the lower side of the separation / heat coking catalyst conduit 41 to recover the heat transfer medium M separated and cooled by the moving fluid to the medium supply unit 10. As an example, the recovery line 42 is inclined to connect the upper separation / heating caulking catalyst line 41 to the lower medium inlet line 22. Therefore, the cooled heat transfer medium M is circulated to the medium supply unit 10 via the recovery line 42.

5 is a detailed view of the catalyst regeneration unit of FIG. 1. 1 and 5, the catalyst regeneration unit 50 is configured to regenerate the heated coking catalyst supplied from the separation unit 40 by burning residual coke by a second combustion operation.

For example, the catalyst regeneration unit 50 includes a second chamber 51, a coking catalyst inlet conduit 52, and a regeneration catalyst conduit 53. The second chamber 51 forms a second combustion space BS2 which burns and regenerates coke remaining in the heated caulking catalyst.

The caulking catalyst inlet conduit 52 is connected to the separator 40, that is, the separation / heating caulking catalyst conduit 41, and extends inside the second chamber 51 to introduce the caulking catalyst separated and heated together with the moving fluid. do.

That is, the caulking catalyst inlet pipe 52 connects the separation / heating caulking catalyst pipe 41 and the second chamber 51 of the separating part 40, and further extends inside the second chamber 51 so that one end thereof is formed. It is exposed and opened inside the two chamber 51.

As an example, the regenerated catalyst pipeline 53 is inclined and connected to the upper catalyst regenerator 50 to supply the regenerated catalyst in the second combustion space BS2 to the lower front process. That is, the regeneration catalyst pipe 53 connects the catalyst regeneration unit 50 with the preceding process.

On the other hand, the catalyst regeneration unit 50, the second air supply line 54 and the second fuel supply line for supplying air and fuel to the second combustion space (BS2), respectively, in order to burn the residual coke by the second combustion action. It further includes (55).

The second air supply conduit 54 and the second fuel supply conduit 55 supply air and fuel from the outside, burn in the second combustion space BS2 of the second chamber 51, and supply the heated caulking. It is possible to burn off the coke remaining in the catalyst. In this case, only fuels H ₂ , CO, and carbon that can prevent after-burning may be used.

The second air supply conduit 54 and the second fuel supply conduit 55 have a donut shape disposed outside the caulking catalyst inlet conduit 52 in the second chamber 51 and include a plurality of nozzles. As a result, the air and the fuel are uniformly injected to enable a uniform second combustion operation in the second combustion space BS2.

In addition, the catalyst regeneration unit 50 flows the moving fluid supplied to the second chamber 51 and the heated caulking catalyst into the cyclone 56 installed therein, and separates the moving fluid from the caulking catalyst.

The separated moving fluid is discharged out of the second chamber 51, the coking catalyst is regenerated via the second chamber 51, and supplied to the preceding process through the regeneration catalyst conduit 53. In this way, the catalyst regeneration unit 50 regenerates the catalyst by burning carbon remaining in the coking catalyst by the second combustion action.

Hereinafter, a method of regenerating a coking catalyst using the catalyst regeneration apparatus of FIGS. 1 to 5 will be described.

6 is a flowchart of a catalyst regeneration method of a circulating heat exchange method according to an embodiment of the present invention. Referring to Figure 6, the cyclic heat exchange type catalyst regeneration method of the embodiment is a medium supply step (ST10), medium heating step (ST20), mixing / heat exchange step (ST30), separation step (ST40), and catalyst regeneration step ( ST50) to regenerate the coking catalyst. In the medium supply step ST10, the heat transfer medium M is supplied from the medium supply unit 10 to the medium heating unit 20.

The medium heating step ST20 heats the heat transfer medium M supplied from the medium supplying step ST10. More specifically, the medium heating step (ST20) is a step of introducing the heat transfer medium (M) to the first combustion space (BS1), the heat transfer medium (M) in the first combustion space (BS1) where the fuel and air is supplied. Heating to a high temperature, and feeding the heated high temperature heat transfer medium (M) to the mixing / heat exchange step (ST30).

In the mixing / heat exchange step ST30, the heated heat transfer medium M supplied from the medium heating step ST20 and the coking catalyst supplied after the previous process are mixed and heat exchanged. In the mixing / heat exchange step ST30, the caulking catalyst is introduced into the mixing / heat exchange chamber 31 by the stripper 33, and the high temperature heat transfer medium M heated in the medium heating step ST20 is mixed / heat exchange chamber ( 31), mixing and heat exchange of the incoming caulking catalyst and the high temperature heat transfer medium (M) in the mixing / heat exchange chamber 31, and the coking catalyst heated by mixing with the high temperature heat transfer medium (M) And supplying the cooled heat transfer medium (M) to the separation step (ST40).

Separation step (ST40) separates the mixed caulking catalyst and the heat transfer medium (M) supplied from the mixing / heat exchange step (ST30). Separation step (ST40) separates the heated caulking catalyst and the cooled heat transfer medium (M) introduced in the mixing / heat exchange step (ST30) in the separation / heating caulking catalyst conduit 41 and catalyst regeneration of the separated heated caulking catalyst Supplying to step ST50, and recovering the cooled heat transfer medium M separated in the separation / heating coking catalyst conduit 41 to the medium supplying step ST10.

The catalyst regeneration step ST50 is regenerated by burning residual coke in the heated coking catalyst supplied from the separation step ST40. The catalyst regeneration step ST50 may include introducing a coking catalyst heated in the second combustion space BS2, and burning and regenerating residual coke in the coking catalyst heated in the second combustion space BS2 supplied with fuel and air. And feeding the regenerated catalyst to the previous process. The regenerated catalyst is fed back to the previous process and used for catalysis.

Although the preferred embodiments of the present invention have been described above, the present invention is not limited thereto, and various modifications and changes can be made within the scope of the claims and the detailed description of the invention and the accompanying drawings. Naturally, it belongs to the scope of the invention.

10: medium supply unit 20: medium heating unit
21: first chamber 22: medium inflow pipeline
23: heating medium pipeline 24: first air supply pipeline
25: first fuel supply line 30: mixing / heat exchange unit
31 mixing / heat exchange chamber 32 caulking catalyst duct
33: stripper 34: mixing duct
40: Separation part 41: Separation / heating caulking catalyst pipe
42: recovery line 50: catalyst regeneration unit
51: second chamber 52: caulking catalyst inlet conduit
53: regenerated catalyst pipeline 54: second air supply pipeline
55: 2nd fuel supply line BS1: 1st combustion space
BS2: second combustion space M: heat transfer medium
MHS: Mix / Heat Exchange Space

Claims (14)

A medium supply unit supplying a heat transfer medium;
A medium heating unit for heating the heat transfer medium supplied from the medium supply unit by a first combustion operation;
A mixing / heat exchange unit for mixing the heated heat transfer medium supplied from the medium heating unit with the caulking catalyst supplied after the previous process and mutually exchanging heat;
A separation unit separating the mixed caulking catalyst and the heat transfer medium supplied from the mixing / heat exchange unit; And
Catalyst regeneration unit for regenerating the coking catalyst supplied from the separation unit by burning the residual coke by the second combustion action
Catalyst regenerator of the circulation heat exchange method comprising a. The method of claim 1,
The heat transfer medium is
Greater specific gravity than the catalyst,
Formed of alumina balls or metal balls with large heat capacity
Catalyst regenerator with circulating heat exchange. The method of claim 1,
The above process
Fluid catalyst cracking (FCC) olefin production process,
The first combustion unit
Using methane generated as a byproduct in the process
Catalyst regenerator with circulating heat exchange. The method of claim 1,
The medium heating unit
A first chamber forming a first combustion space,
A medium inlet conduit connected to the medium supply unit and extending inside the first chamber to introduce the heat transfer medium; and
Heating medium pipe for supplying the hot heat transfer medium heated in the first combustion space to the mixing / heat exchange unit
Catalyst regenerator of the circulation heat exchange method comprising a. The method of claim 4, wherein
The medium heating unit
A first air supply line and a first fuel supply line for supplying air and fuel to the first combustion space, respectively, for the first combustion operation;
Catalyst regenerator of the circulation heat exchange method further comprising. The method of claim 1,
The mixing / heat exchange part
A mixing / heat exchange chamber forming a mixing / heat exchange space, and
Coking catalyst conduit connected to the upper side of the mixing / heat exchange chamber to supply a coking catalyst from the stripper
Including,
Heating medium conduit for supplying a high temperature heat transfer medium from the first chamber
Connected to the caulking catalyst conduit,
The mixing / heat exchange chamber
Connected to the separator via a mixing conduit that is mixed with a hot heat transfer medium to supply a heated caulking catalyst.
Catalyst regenerator with circulating heat exchange. The method of claim 1,
The separating part
A separation / heating caulking catalyst pipeline which separates the heated caulking catalyst and the cooled heat transfer medium connected to the mixing / heat exchange chamber and is fed to the catalyst regeneration unit by feeding the separated and heated caulking catalyst to the catalyst regeneration unit.
A recovery conduit connected to the lower side of the separation / heat coking catalyst conduit to recover the separated and cooled heat transfer medium to the medium supply unit.
Catalyst regenerator of the circulation heat exchange method comprising a. The method of claim 1,
The catalyst regeneration unit
A second chamber forming a second combustion space,
A caulking catalyst inlet conduit extending into the second chamber so as to introduce a caulk catalyst separated and heated connected to the separator; and
Regenerated catalyst pipeline for supplying regenerated catalyst to the previous process by burning residual coke in the second combustion space
Catalyst regenerator of the circulation heat exchange method comprising a. The method of claim 8,
The catalyst regeneration unit
A second air supply line and a second fuel supply line for supplying air and fuel to the second combustion space, respectively, for the second combustion operation;
Catalyst regenerator of the circulation heat exchange method further comprising. A medium supplying step of supplying a heat transfer medium;
A medium heating step of heating the heat transfer medium supplied from the medium supplying step;
A mixing / heat exchange step of mixing the heated heat transfer medium supplied from the medium heating step with the caulking catalyst supplied after the preceding process and mutually exchanging heat;
A separation step of separating the mixed coking catalyst and the heat transfer medium supplied from the mixing / heat exchange step; And
Catalyst regeneration step for regenerating by burning residual coke in the heated coking catalyst supplied from the separation step
Catalyst regeneration method of the circulation heat exchange method comprising a. The method of claim 10,
The medium heating step
Introducing the heat transfer medium into a first combustion space;
Heating the heat transfer medium to a high temperature in the first combustion space to which fuel and air are supplied, and
Feeding the heated hot heat transfer medium to the mixing / heat exchange step
Catalyst regeneration method of the circulation heat exchange method comprising a. The method of claim 10,
The mixing / heat exchange step
Introducing the coking catalyst from the stripper into the mixing / heat exchange chamber,
Introducing a high temperature heat transfer medium heated in the medium heating step into the mixing / heat exchange chamber;
Mixing / heat exchange of the incoming caulking catalyst and the high temperature heat transfer medium in a mixing / heat exchange chamber, and
Feeding the coking catalyst heated by mixing with a high temperature heat transfer medium together with the cooled heat transfer medium to the separation step
Catalyst regeneration method of the circulation heat exchange method comprising a. The method of claim 10,
The separation step
Separating the heated coking catalyst and the cooled heat transfer medium introduced in the mixing / heat exchange step from the separation / heat coking catalyst pipeline and supplying the separated heated coking catalyst to the catalyst regeneration step, and
Recovering the cooled heat transfer medium separated in the separation / heating coking catalyst pipeline to a medium feed stage
Catalyst regeneration method of the circulation heat exchange method comprising a. The method of claim 10,
The catalyst regeneration step
Introducing a caulking catalyst heated to the second combustion space,
Burning and regenerating residual coke in a coking catalyst heated in the second combustion space supplied with fuel and air, and
Feeding the regenerated catalyst into the previous process
Catalyst regeneration method of the circulation heat exchange method comprising a.

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