KR20190129298A - Catalyst regenerator - Google Patents

Abstract

Provided by an embodiment of the present invention is a catalyst regenerator which has an autothermal reforming reactor capable of supplying gaseous fuel (i.e., autothermally reformed gaseous fuel) into powdered coking catalysts, and maintains the minimum size of bubbles of gaseous fuel. According to an embodiment of the present invention, the catalyst regenerator causes a heat absorption catalyst reaction in a fluidized bed reactor, separates catalysts from generated products, and raises the temperature of catalysts or oxidizes byproducts on the surface of catalysts. The present invention includes: a container setting the regeneration space of catalysts and supplying, through an outlet, regenerated catalysts of which the temperature is increased and byproducts on the surface thereof are removed; an air supply unit installed in the regeneration space to inject air to catalysts supplied to the regeneration space; an autothermal reforming reactor receiving separation gas fuel containing methane separated from the product of the heat absorption catalyst reaction as a main component, and autothermally reforming catalysts in a reforming container; and a gas fuel supply unit connected to the autothermal reforming reactor, installed in the regeneration space in the upper side of the air supply unit, and injecting gas fuel reformed with hydrogen and carbon monoxide supplied from the autothermal reforming reactor as main components to catalysts of the regeneration space.

Description

Catalytic Regenerator {CATALYST REGENERATOR}

TECHNICAL FIELD The present invention relates to a catalyst regenerator, and more particularly, a gaseous fuel (ie, autothermally reformed gaseous fuel) inside a powdered coking catalyst when regenerating a coking catalyst during a fluidized bed reaction process using a catalytic cracking system. A catalyst regenerator having an autothermal reforming reactor capable of supplying C) and maintaining a minimum bubble size of gas fuel to accelerate combustion and heat transfer of the reformed gas fuel in a catalyst dense zone. will be.

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.

Olefin (olefin) is obtained through the decomposition of naphtha (naphtha) or from ethane. In our country mainly produced naphtha to produce olefin compounds such as ethylene.

Conventionally, olefins were produced in naphtha by performing a process at a high temperature of 1000 ° C. or more using a pyrolysis process (naphtha cracking center (NCC) naphtha cracking process).

Recently, a process for producing olefins from naphtha at lower temperatures of about 700 ° C using a catalyst has been commercialized.

In the case of using a catalyst, for example, naphtha is supplied to the bottom of the riser together with steam, and a regenerated catalyst pushed out of the catalyst regenerator is supplied to the bottom of the riser, so that naphtha and catalyst are mixed to rise up the riser. The decomposition reaction of continues.

The riser is connected to a cyclone provided on top of the catalyst regenerator. The olefin gas thus produced is separated in the cyclone, and the caulked catalyst is separated in the cyclone and falls down through a stripper vessel and accumulates at the bottom of the regenerator.

The catalyst is coked in the course of naphtha cracking in the riser. That is, carbon particles cover the surface of the catalyst. Other types of fluidized bed reactors other than naphtha cracking generate a significant amount of carbon particles in the reaction at several percent by weight of the catalyst.

The catalyst must be recycled and then sent back to the riser to be mixed with naphtha to undergo a cycle used for the decomposition reaction of naphtha. When the catalyst is coked, however, it is difficult to smoothly cause naphtha decomposition.

Thus, the caulked catalyst dropped to the bottom of the catalyst regenerator is regenerated. In other words, regeneration burns off the carbon particles attached to the catalyst. The calorific value generated at this time can be obtained a temperature rise of about 40 ~ 60 ℃ during the catalyst regeneration process.

The naphtha decomposition reaction that occurs in the riser is an endothermic reaction, so the temperature rises to the top of the riser and the reaction temperature drops by about 40 to 50 ° C. The lowered temperature in this process must be compensated for by the exotherm in the regeneration of the catalyst.

Therefore, for regenerating the catalyst, hot air is supplied from the lower end of the catalyst regenerator. The supplied hot air burns carbon particles to induce regeneration of the coked catalyst. The regenerated catalyst is fed back to the riser to be used for cracking naphtha.

Naphtha is classified into light naphtha and heavy naphtha according to the carbon content. In the case of light naphtha, the amount of carbon particles generated in the catalytic naphtha decomposition process is less than 1%.

Since the amount of carbon particles generated is less than about 1%, even when all of the carbon particles are burned, a temperature rise of about 40 to 60 ° C. is not realized. Therefore, in the naphtha cracking process using a fluidized bed catalyst, liquid fuel is injected into the catalyst, hot air is supplied to the catalyst in contact with the liquid fuel, and the fuel is further burned to generate heat. The way to make it work is being adopted.

That is, there is a method of supplying a liquid fuel by spraying the catalyst fluidized bed in powder form. In this case, the dispersion performance of the liquid fuel is low, and thus hot spots may occur. Hot spots reduce the regeneration performance of the catalyst by exposing the catalyst fluidized bed to high temperatures, and increase the catalyst replacement cycle due to damage of the catalyst by high temperature exposure.

In one embodiment of the present invention, when regenerating a caulked catalyst during a fluidized bed catalytic reaction process using a catalytic cracking system, a gaseous fuel (ie, auto-reformed gaseous fuel) reformed inside a powdered caulked catalyst is used. It is to provide a catalytic regenerator having a supply of autothermal reforming reactor, to minimize the bubble size of the gas fuel, to accelerate the combustion and heat transfer of the reformed gas fuel in the catalyst dense zone .

Catalyst regenerator according to an embodiment of the present invention, after the endothermic catalytic reaction in the fluidized bed reactor, the catalyst and the resulting product is separated, the temperature of the catalyst is raised or the by-products on the surface of the catalyst, the regeneration space of the catalyst And a vessel for supplying the regenerated catalyst having the temperature increased through the outlet and removing the by-product from the surface of the catalyst, an air supply unit installed in the regeneration space to inject air to the catalyst supplied to the regeneration space, and the endothermic catalyst. The autothermal reforming reactor subjected to autothermal reforming reaction in a reforming catalyst built in a reforming vessel by receiving a separator gas fuel containing methane separated from the product of the reaction, and connected to the autothermal reforming reactor and the regeneration above the air supply unit. A group which is installed in a space and is mainly modified with hydrogen and carbon monoxide supplied from the autothermal reforming reactor It includes a gas fuel supply unit for injecting a body fuel to the catalyst of the regeneration space.

The outlet may be installed at a height set from the bottom of the vessel, and the regeneration space may include a catalyst dense zone set at a height lower than the outlet, and a catalyst thinning zone set at an upper side of the outlet.

The vessel has a perforate plate (perforate plate) on the upper side of the gas fuel supply unit, the porous plate may be provided in a single layer or multiple layers in the catalyst dense region.

The air supply unit includes an air distribution ring installed in the catalyst concentration region and an air orifice formed in the air distribution ring, and the gas fuel supply portion is a fuel distribution ring installed corresponding to the air distribution ring in the catalyst concentration region. And it may include a fuel orifice formed in the fuel distribution ring.

The vessel forms a convex bottom downward, and the stand pipe for supplying the separated catalyst is installed in the center of the vessel in the vertical direction at the center of the air distribution ring and the fuel distribution ring, and the bottom of the stand pipe. The opening may form a predetermined gap with the bottom.

The autothermal reforming reactor may be further supplied with air and water in addition to the separator gas.

The autothermal reforming reaction of the autothermal reforming reactor may be operated at an O ₂ / CH ₄ ratio of 0.5 to 1.0, which is equal to or higher than the O ₂ / CH ₄ ratio of 0.5, which is a partial oxidation condition.

The autothermal reforming reactor may be further supplied with an external gas fuel (eg, methane) from the outside of the reforming vessel in addition to the separator gas fuel.

The autothermal reforming reactor may include a pilot burner or an igniter in which the O ₂ / CH ₄ ratio starts a combustion reaction at 2.0 in the reforming vessel.

The autothermal reforming reactor may connect an external combustor for supplying a high temperature combustion product gas therein to the reforming vessel.

The autothermal reforming reactor is provided in the reforming vessel to which the separator gas and the air are supplied, the first mixer for mixing the separator gas and the air, and provided in a downstream direction of the first mixer to supply water supplied to the reforming vessel. It may include a water supply for spraying, a second mixer provided between the upstream direction of the reforming catalyst and the water supply in the reforming container to mix the separator gas and air and water.

The autothermal reforming reactor is provided in the reforming vessel supplied with the separator gas and air, and is provided between the mixer for mixing the separator gas and the air, and between the upstream direction of the reforming catalyst embedded in the reforming vessel and the mixer. It may include a water supply unit for spraying water supplied in the downstream direction of the reforming vessel.

The water supply unit may further include a heat exchanger connected to a downstream direction of the reforming vessel and exchanging heat in a large area inside the reforming vessel.

As described above, in one embodiment of the present invention, the autothermal reforming reactor receives a separator gas fuel containing methane separated from the product of the endothermic catalytic reaction as a main component and performs autothermal reforming reaction in a reforming catalyst embedded in the reforming vessel, and gaseous fuel. The supply unit injects gaseous fuel reformed mainly from hydrogen and carbon monoxide supplied from the autothermal reforming reactor to the catalyst in the regeneration space.

Therefore, one embodiment may increase the temperature through the combustion of stable hydrogen and carbon monoxide even in the catalyst dense zone of the powdered caulked catalyst (catalyst dense zone).

One embodiment may include a porous plate inside the catalyst regenerator to keep the bubble size of the reformed gas fuel to a minimum. Thus, one embodiment may accelerate the combustion and heat transfer of the reformed gaseous fuel in a catalyst dense zone.

In addition, in one embodiment, when methane, one of the gaseous fuels, is used as a separate gas fuel (eg, most of hydrocarbon fuels (eg, naphtha, propane, etc.), a gas reformed using methane generated as a by-product from a fluidized bed reactor Fuel) and the cost of regenerating the coked catalyst can be reduced.

1 is a block diagram of a catalyst regenerator according to a first embodiment of the present invention.
2 is a block diagram of an autothermal reforming reactor applied to a catalyst regenerator according to a second embodiment of the present invention.
3 is a configuration diagram of an autothermal reforming reactor applied to a catalyst regenerator according to a third embodiment of the present invention.
FIG. 4 is a driving flowchart of the autothermal reforming reactor applied to FIG. 3.
5 is a configuration diagram of an autothermal reforming reactor applied to a catalyst regenerator according to a fourth embodiment of the present invention.
FIG. 6 is a flow chart illustrating an autothermal reforming reactor applied to FIG. 5.
7 is a configuration diagram of an autothermal reforming reactor applied to a catalyst regenerator according to a fifth embodiment of the present invention.
8 is a configuration diagram of an autothermal reforming reactor applied to a catalyst regenerator according to a sixth 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.

Although not shown, a fluidized bed reactor using a catalytic cracking system mixes reactants and catalyst in a riser (not shown) to cause a cracking reaction of the reactants, and then separates the caulked catalyst and the product into cyclones to convert the caulked catalyst into a catalyst regenerator. Drop it.

In one embodiment, the process for producing olefins using naphtha as a reactant may be performed by mixing naphtha and a catalyst, causing naphtha decomposition reactions, and then separating the caulked catalyst and the produced olefin from a cyclone (not shown) and caulking. The catalyst is dropped into the catalyst regenerator (see FIG. 1).

In other words, naphtha is injected into the lower part of the riser together with steam and meets a high temperature catalyst (including a regenerated catalyst), and naphtha begins to be decomposed through a catalytic reaction. Naphtha continues to endothermally decompose while rising along the riser.

After the naphtha decomposition reaction, the catalyst covered with solid carbon particles, that is, the coked catalyst and the olefin produced in the decomposition reaction, enter the cyclone and are separated from each other. The caulked catalyst separated from the cyclone is taken down the stand pipe 10 (see FIG. 1) into the catalyst regenerator of one embodiment provided below.

In a fluidized bed reactor, the catalyst regenerator plays two major roles. The first role is to oxidize the byproducts of the catalyst surface from the main reaction of the fluidized bed reactor in a high temperature environment.

The catalyst regenerator regenerates the caulked catalyst. The main component of the by-product formed on the surface of the catalyst is carbon particles, which in some cases may include hydrocarbon-based materials that could not be removed.

The second role is to replenish the amount of heat required for the main reaction by raising the temperature of the catalyst in the catalyst regenerator when the main reaction of the fluidized bed reactor is endothermic. For example, the main reaction may be naphtha cracking or dehydration to convert propane to propylene.

In this case, the main reactions are all endothermic. Therefore, in order to make up for the additional heat required in the catalyst regenerator, it is necessary to burn fuel and make up the heat supply.

Catalyst regenerators may be used to play the first and second roles simultaneously or to achieve only the second role.

The catalyst regenerator may be configured to cause endothermic catalysis in a fluidized bed reactor, to separate the caulked catalyst and the resulting product, to raise the temperature of the caulked catalyst or to oxidize the byproducts of the caulked catalyst surface.

1 is a block diagram of a catalyst regenerator according to an embodiment of the present invention. Referring to FIG. 1, the catalyst regenerator of the first embodiment includes a vessel 20, an air supply unit 30, an auto-thermal reforming reactor 40, and a gas fuel supply unit 50.

The vessel 20 sets the regeneration space S of the catalyst, and through the outlet 21 provided on one side, the temperature is increased, and by-products (carbon particles) on the surface of the caulked catalyst are removed. That is, to supply the regenerated catalyst to the riser.

The outlet 21 connects the vessel 20 below the riser to supply regenerated catalyst to the riser. The outlet 21 is installed at a height H set from the bottom of the container 20.

The vessel 20 has a perforate plate 22 above the gaseous fuel supply 50. Accordingly, the regeneration space S includes a catalyst dense zone Z1 set at a height lower than the outlet 21, and a catalyst lean zone Z2 set at an upper side of the outlet 21.

As an example, the porous plate 22 may be provided in a single layer or multiple layers in the catalyst dense zone Z1. The porous plate 22 allows the catalyst regenerated in the catalyst dense zone Z1 to be continuously supplied to the outlet 21 while preventing the backflow of the regenerated catalyst.

The porous plate 22 is installed inside the vessel 20 to form a bubbling bed in the regeneration space S, so that the gaseous fuel, combustion mixture, and the like modified in the powdered coking catalyst are formed. It is possible to keep the bubble size of the reaction product to a minimum.

The air supply unit 30 is installed in the regeneration space S to enable combustion of the caulked catalyst supplied to the regeneration space S, and to inject air for the combustion into the regeneration space S. The air supply unit 30 injects air to the caulked catalyst in the regeneration space (S).

The gas fuel supply unit 50 is installed in the regeneration space S to supply gas fuel for combustion to the regenerated space S to the coked catalyst in the regeneration space S. The gas fuel supply unit 50 injects the reformed gas fuel into the air.

Therefore, the air injected from the air supply unit 30 and the gas fuel supply unit 50 and the reformed gas fuel are burned in the regeneration space S, and the carbon particles of the caulked catalyst are burned to regenerate the coked catalyst.

For example, the air supply unit 30 includes an air distribution ring 31 and an air orifice 32 installed in the catalyst dense zone Z1. Air distribution ring 31 is formed along the circumferential direction in the interior of the container 20 is disposed in the circumferential direction.

The air orifice 32 is provided in the air distribution ring 31 and provided downward in the catalyst dense zone Z1 to inject air downward. The air orifice 32 is provided in plural, spaced apart along the circumferential direction of the air distribution ring 31, and uniformly injects and supplies air in the circumferential direction inside the vessel 20, so that the catalyst density zone Z1. Allows uniform flame and catalyst to be uniformly regenerated in the circumferential direction.

The gas fuel supply unit 50 includes a fuel distribution ring 51 and a fuel orifice 52. The fuel distribution ring 51 is installed above the air supply unit 30 in the catalyst dense zone Z1. The fuel distribution ring 51 is formed along the circumferential direction corresponding to the air distribution ring 31 and disposed in the circumferential direction.

A plurality of fuel orifices 52 are provided in the fuel distribution ring 51 to downwardly inject the reformed gas fuel into the catalyst dense zone Z1. The fuel orifice 52 is spaced apart on the fuel distribution ring 51 along the circumferential direction, and uniformly injects and supplies the reformed gas fuel in the circumferential direction of the container 20, thereby providing a circumference of the catalyst density region Z1. Enables uniform flame and catalyst uniform regeneration in the direction.

The vessel 20 forms a bottom 23 that is convex downward. That is, the inside of the bottom 23 is formed in an upward concave structure. The stand pipe 10 supplies a caulked catalyst separated from the product of the endothermic catalytic reaction to the vessel 20, for this purpose, in the center of the vessel 20, an air distribution ring 31 and a fuel distribution ring 51. It is installed in the vertical direction in the center of the. The air distribution ring 31 is connected to the air pipe 311 and is drawn out of the container 20.

The bottom opening of the stand pipe 10 forms a set gap G with the bottom 23. Therefore, the caulked catalyst supplied to the opening of the stand pipe 10 is supplied to the regeneration space S formed as the bottom 23 concave upward through the gap G. The concave bottom 23 distributes the upward flow uniformly in the circumferential direction while facilitating the conversion of the upward flow after the downward flow of the caulked catalyst.

The caulked catalyst supplied to the stand pipe 10 is mixed with the air supplied from the air distribution ring 31 and further mixed with the reformed gas fuel supplied from the fuel distribution ring 51.

At this time, the porous plate 22 keeps the bubble size of the combustion mixture and the reaction product of the reformed gaseous fuel in the powdered caulked catalyst by the catalyst, the air and the reformed gaseous fuel to a minimum. Therefore, heat transfer and combustion of the reformed gas fuel in the catalyst compaction zone Z1 can be accelerated.

In the regeneration space S, the catalyst density zone Z1 under the porous plate 22 is set below the outlet 21 to intensively burn and regenerate the caulked catalyst, and the catalyst thinning above the porous plate 22. Zone Z2 is set above the outlet 21 to minimize after-burning.

To this end, the autothermal reforming reactor (40) is supplied with a separator gas fuel mainly composed of methane separated from the product of the endothermic catalytic reaction to perform the autothermal reforming reaction in the reforming catalyst (42) embedded in the reforming vessel (41). .

The reforming vessel 41 is connected to the gas fuel supply unit 50 through the connection pipe 411, and supplies the reformed gas fuel to the gas fuel supply unit 50 in the autothermal reforming reactor 40. The reformed gaseous fuel is combusted in the catalyst regenerator, which leads to an increase in the surface temperature of the caulked catalyst to accelerate the combustion of carbon formed on the surface.

The gas fuel supply unit 50 is connected to the autothermal reforming reactor 40 and is installed in the regeneration space S above the air supply unit 30. The autothermal reforming reactor 40 reforms the separator gas fuel and supplies the reformed gas fuel.

The gaseous fuel supply unit 50 injects the gaseous fuel modified with hydrogen and carbon monoxide supplied from the autothermal reforming reactor 40 to the coked catalyst in the regeneration space S to regenerate the catalyst.

On the other hand, the autothermal reforming reaction requires a reactant separator gas fuel and air and water (moisture). Therefore, the autothermal reforming reactor 40 is further supplied with air and water (moisture) in addition to the separator gas fuel.

Moisture can increase the durability of the reforming catalyst 42 by controlling the temperature and removing carbon generated on the surface of the reforming catalyst 42 in the catalytic reaction of the reforming catalyst 42 in the autothermal reforming reactor 40. .

The general partial oxidation catalytic reforming reaction generates hydrogen and carbon monoxide using gaseous methane and air as reactants. However, the partial oxidation catalytic reforming reaction causes a decrease in catalyst performance and pipe blockage due to carbon formation on the surface of the catalyst.

On the other hand, in the first embodiment, the autothermal reforming reaction of the autothermal reforming reactor 40 is operated at an O ₂ / CH ₄ ratio of 0.5 to 1.0, which is equal to or higher than the O ₂ / CH ₄ ratio of 0.5, which is a partial oxidation condition.

Compared with the general partial oxidation catalytic reforming reaction, the autothermal reforming reaction of the first embodiment additionally supplies water (moisture) to the partial oxidation catalytic reforming to further generate hydrogen by supplying a heat source for the catalytic reaction and reacting water with carbon. And it may have the advantage of further removing carbon through carbon combustion.

After endothermic catalysis in the fluidized bed reactor, the separated gaseous fuel is reused and reformed through the autothermal reforming reaction of the autothermal reforming reactor 40, and the reformed gaseous fuel mainly composed of hydrogen and carbon monoxide is introduced into the catalyst regenerator. It is fed and burned with carbon particles on the surface of the caulked catalyst.

In the first embodiment, since an additional heat source or power is not required through the autothermal reforming reaction, operation of the catalyst regenerator can be realized with minimum energy.

Hereinafter, various embodiments of the present invention will be described. By comparing the following embodiments with the first embodiment and the previously described embodiments, the same configuration will be omitted, and different configurations will be described.

2 is a block diagram of an autothermal reforming reactor applied to a catalyst regenerator according to a second embodiment of the present invention. Referring to FIG. 2, the autothermal reforming reactor 240 applied to the catalyst regenerator of the second embodiment has a structure of the autothermal reforming reactor 40 of the first embodiment, which receives the separator gas, from the outside of the reforming container 41. More gaseous fuel (eg methane, not gas) is supplied. In other words, the reforming vessel 41 is supplied with a separate gas fuel and an external gas fuel.

The autothermal reforming reaction of the autothermal reforming reactor 240 is higher than the O ₂ / CH ₄ ratio 0.5 of the partial gas and the external gas fuel, which is a partial oxidation condition, and lower than the O ₂ / CH ₄ ratio 2.0 of the combustion condition. It is operated and undergoes a partial combustion reaction of gaseous fuel (eg methane) and external gaseous fuel.

At this time, the generated heat is utilized as a heat source of the reforming catalyst 42. The additionally supplied water (moisture) reacts with the carbon to inhibit carbon formation on the surface of the reforming catalyst 42, or reacts with methane to generate hydrogen and carbon dioxide.

In the autothermal reforming reactor 240, the gaseous fuel reformed from the separator gas and the external gaseous fuel is supplied to the inside of the catalyst regenerator through the connecting pipe 411 and burned together with the carbon particles on the surface of the caulked catalyst.

FIG. 3 is a configuration diagram of an autothermal reforming reactor applied to a catalyst regenerator according to a third embodiment of the present invention, and FIG. 4 is a driving flowchart of the autothermal reforming reactor applied to FIG. 3. 3 and 4, the autothermal reforming reactor 340 applied to the catalyst regenerator of the third embodiment has a pilot burner or igniter in the structure of the autothermal reforming reactor 40 of the first embodiment. 344 is further provided to the reforming container 41.

A pilot burner or igniter 344 is provided inside (upper side) of the reforming vessel 41 so that the O ₂ / CH ₄ ratio of the separator gas fuel starts the combustion reaction at 2.0.

The driving sequence of the autothermal reforming reactor 340 includes a first step ST1, a second step ST2, a third step ST3, and a fourth step ST4. The first step ST1 uses a pilot burner or igniter 344 to start the combustion reaction at an O ₂ / CH ₄ ratio of the separator gas of 2.0.

The second step (ST2) is to reduce the O ₂ / CH ₄ ratio of the separator gas by 2.0 step by step, maintaining the 1.0 or more to utilize the heat of combustion generated in the combustion reaction zone of the autothermal reforming reactor 340, 41) heat up the interior of the chamber.

The third step ST3 stabilizes the temperature distribution inside the reforming vessel 41 by supplying water (water) to the autothermal reforming reactor 340.

The fourth step (ST4) is to gradually reduce the O ₂ / CH ₄ ratio of the separator gas fuel to convert to the separator gas (eg methane) reforming zone, the temperature of the reforming vessel 41, and the separator gas fuel (eg select the optimum O ₂ / CH ₄ ratio in accordance with methane) conversion rate, and operating in a predetermined ratio.

That is, the autothermal reforming reactor 340 supplies the reformed gas reformed from the separator gas fuel (eg, methane) to the catalyst regenerator through the connecting pipe 411. The reformed gas supplied is combusted with the carbon particles of the coked catalyst inside the catalyst regenerator.

FIG. 5 is a configuration diagram of an autothermal reforming reactor applied to a catalyst regenerator according to a fourth embodiment of the present invention, and FIG. 6 is a flowchart illustrating an operation of the autothermal reforming reactor applied to FIG. 5. 5 and 6, the autothermal reforming reactor 440 applied to the catalyst regenerator of the fourth embodiment includes an external combustor 444 in the reforming vessel 41 in the structure of the autothermal reforming reactor 40 of the first embodiment. Connect more.

The external combustor 444 is connected to the reforming vessel 41 (upper part) to supply hot combustion product gas into the reforming vessel 41.

The driving sequence of the autothermal reforming reactor 440 includes a first step ST21, a second step ST22, a third step ST23, and a fourth step ST24. In the first step ST21, the high temperature combustion product gas is supplied into the reforming vessel 41 of the autothermal reforming reactor 440 by utilizing the external combustor 444.

In the second step ST22, the temperature of the reforming vessel 41 is stabilized by supplying air and water (moisture) at a temperature of about 700 ° C. in the reforming vessel 41 of the autothermal reforming reactor 440.

In the third step ST23, the separator gas is supplied into the reforming vessel 41 to perform an autothermal reforming reaction, and the temperature of the reforming vessel 41 is stabilized by controlling the O ₂ / CH ₄ ratio in the separator gas. In addition, the combustion gas in the external combustor 444 is blocked.

In the fourth step ST24, the temperature stabilization and the generated reformed gas are supplied into the catalyst regenerator through the connection pipe 411 and burned together with the carbon particles of the caulked catalyst.

7 is a configuration diagram of an autothermal reforming reactor applied to a catalyst regenerator according to a fifth embodiment of the present invention. Referring to FIG. 7, the autothermal reforming reactor 540 applied to the catalyst regenerator of the fifth embodiment includes a reforming vessel 41, a first mixer 541, a water supply unit 543, and a second mixer 542. .

The first mixer 541 is provided inside (upward) of the reforming vessel 41, and mixes the separator gas and air supplied (from above) to start a uniform combustion reaction in the reforming vessel 41. To be.

The water supply part 543 is provided in the downstream direction of the first mixer 541 and sprays water (water) supplied to the reforming container 41 (from the side) to the inside of the reforming container 41. The water supply unit 543 uniformly supplies water (water) into the reforming container 41 and stabilizes the temperature distribution inside the reforming container 41 through water (water) supply.

The second mixer 542 is provided between the upstream direction of the reforming catalyst 42 embedded in the reforming vessel 41 and the water supply section 543, and uniformly separates the gas fuel, air, and water (moisture). It is mixed and supplied to the built-in reforming catalyst 42 to enable a uniform catalytic reaction of the reforming catalyst 42. The reformed reformed gas is fed into the catalyst regenerator through the connection pipe 411 and combusted with the carbon particles of the caulked catalyst.

8 is a configuration diagram of an autothermal reforming reactor applied to a catalyst regenerator according to a sixth embodiment of the present invention. Referring to FIG. 8, the autothermal reforming reactor 640 applied to the catalyst regenerator of the sixth embodiment includes a reforming vessel 41, a mixer 642, and a water supply unit 643.

The mixer 642 is provided in the reforming vessel 41 (upward inside) to mix the separator gas and the air supplied from the upstream direction so as to start a uniform combustion reaction inside the reforming vessel 41. .

The water supply unit 643 is provided between the upstream direction of the reforming catalyst 42 incorporated in the reforming vessel 41 (lower portion) and the mixer 642, and is supplied to the reforming vessel 41 (downward). (Moisture) is sprayed to stabilize the temperature distribution inside the reforming vessel 41.

In addition, the water supply unit 643 uniformly supplies water (moisture) into the reforming vessel 41, and uniformly mixes the separator gas, air, and water (moisture), and uniformly mixes the reforming catalyst 42 embedded therein. Feeding the mixture enables uniform catalysis of the reforming catalyst 42

The water supply unit 643 further includes a heat exchanger 644 connected from a downstream direction of the reforming vessel 41 and exchanging heat in a large area inside the reforming vessel 41. The heat exchange part 644 makes the temperature distribution of the reforming catalyst 42 more uniform in the reforming container 41 due to the heat exchange action in the reforming container 41, and uniform catalytic reaction of the reforming catalyst 42. To make it possible.

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: stand pipe 20: vessel
21: exit 22: perforate plate
23: bottom 30: air supply
31: Air distribution ring 32: Air orifice
40, 240: autothermal reformer 340, 440, 540, 640: autothermal reformer
41: reforming container 42: reforming catalyst
50: gas fuel supply unit 51: fuel distribution ring
52: fuel orifice 311: air pipe
344: pilot burner or lighter 411: connector
444: external combustor 541, 542: first and second mixer
543, 643: water supply 642: mixer
644: heat exchanger G: gap
H: Height S: Playback Space
Z1: catalyst dense zone Z2: catalyst lean zone

Claims (13)

In a catalyst regenerator which generates an endothermic catalytic reaction in a fluidized bed reactor, separates the catalyst from the resulting product, raises the temperature of the catalyst or oxidizes the by-products on the surface of the catalyst,
A container for setting a regeneration space of the catalyst and supplying a regenerated catalyst having a temperature rise through the outlet and by-products of the catalyst surface removed;
An air supply unit installed in the regeneration space to inject air to the catalyst supplied to the regeneration space;
An autothermal reforming reactor which receives a separator gas fuel mainly composed of methane separated from the product of the endothermic catalytic reaction and undergoes autothermal reforming reaction in a reforming catalyst embedded in a reforming vessel; And
A gas fuel supply unit connected to the autothermal reforming reactor and installed in the regeneration space above the air supply unit to inject a gas fuel modified with hydrogen and carbon monoxide supplied from the autothermal reforming reactor as a main component to the catalyst of the regeneration space;
Catalyst regenerator comprising a. The method of claim 1,
The exit is
Installed at a set height from the bottom of the container,
The playback space is
A catalyst density zone set at a height lower than the outlet, and
Catalyst thinning zone set above the outlet
Catalyst regenerator comprising a. The method of claim 1,
The container
It is provided with a perforate plate (perforate plate) on the upper side of the gas fuel supply,
The porous plate is
Catalyst regenerator provided in the catalyst density region in a single layer or a double layer. The method of claim 2,
The air supply unit
An air distribution ring installed in the catalyst cluster and
An air orifice formed in the air distribution ring,
The gas fuel supply unit
A fuel distribution ring installed corresponding to the air distribution ring in the catalyst dense region;
Fuel orifice formed in the fuel distribution ring
Catalyst regenerator comprising a. The method of claim 4, wherein
The container forms a downwardly convex bottom,
The stand pipe for supplying the separated catalyst is
In the center of the container, is installed in the vertical direction in the center of the air distribution ring and the fuel distribution ring,
The bottom opening of the stand pipe
And a catalyst regenerator forming a set gap with the bottom. The method of claim 1,
The autothermal reforming reactor
A catalyst regenerator receiving air and water in addition to the separator gas. The method of claim 1,
The autothermal reforming reaction of the autothermal reforming reactor
Compared to the partial oxidation condition O ₂ / CH ₄ ratio 0.5
Catalytic regenerator operating at the same or higher conditions O ₂ / CH ₄ ratio 0.5 to 1.0. The method of claim 1,
The autothermal reforming reactor
And a catalyst regenerator further receiving external gas fuel from the outside of the reforming vessel in addition to the separator gas fuel. The method of claim 1,
The autothermal reforming reactor
And a reformer having a pilot burner or igniter in which the O ₂ / CH ₄ ratio starts the combustion reaction at 2.0. The method of claim 1,
The autothermal reforming reactor
A catalyst regenerator for coupling an external combustor for supplying a high temperature combustion product gas to the reformer. The method of claim 1,
The autothermal reforming reactor
A first mixer which is provided in the reforming vessel to which the separator gas and air are supplied and mixes the separator gas and the air,
A water supply unit provided in a downstream direction of the first mixer and spraying water supplied to the reforming container;
A second mixer provided between an upstream direction of the reforming catalyst and the water supply unit incorporated in the reforming container to mix the separator gas with air and water;
Catalyst regenerator comprising a. The method of claim 1,
The autothermal reforming reactor
A mixer provided in the reforming vessel to which the separator gas and air are supplied, for mixing the separator gas and air;
A water supply unit provided between an upstream direction of the reforming catalyst and the mixer built in the reforming container and spraying water supplied from a downstream direction of the reforming container;
Catalyst regenerator comprising a. The method of claim 12,
The water supply unit
A heat exchanger connected to the downstream direction of the reforming vessel and exchanging heat with a large area inside the reforming vessel;
Catalyst regenerator comprising more.

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