JPH02298356A - Method and apparatus for regenerating catalyst - Google Patents

Abstract

PURPOSE:To efficiently regenerate a catalyst by a method wherein a waste catalyst is allowed to fall in the porous fluidizing part in the first-third treatment chambers under gravity and treatment gases are allowed to flow through the respective treatment chambers to successively remove an oil component, a sulfur component and a carbon component. CONSTITUTION:A waste catalyst 1 is allowed to fall through the porous fluidizing part in the first treatment chamber 11 under gravity and passed so as to traverse the fluidizing part 21 while oxygen with concn. of 3% or less is allowed to flow through the treatment chamber 11 at 200-380 deg.C to remove an oil component. Next, the waste catalyst 1 is allowed to fall through the porous fluidizing part 37 in the second treatment chamber 12 continuing to the treatment chamber 11 under gravity and passed so as to cross the fluidizing part 37 while oxygen with concn. of 1.0-5.0% is allowed to flow through the treatment chamber 12 at 300-450 deg.C to remove a sulfur component. Subsequently, the waste catalyst 1 is allowed to fall through the porous fluidizing part 48 in the third treatment chamber 13 continuing to the treatment chamber 12 under gravity and passed so as to cross the fluidizing part 38 while oxygen with concn. of 2.0-10% is allowed to flow through the treatment chamber 13 at 350-600 deg.C to remove a carbon component.

Description

DETAILED DESCRIPTION OF THE INVENTION [Industrial Field of Application J] The present invention relates to a method and apparatus for regenerating a catalyst used in the oil refining industry, petrochemical industry, etc.

[Background Art 1] For example, in the petroleum refining industry, catalysts such as nickel, cobalt, and molybdenum are used for hydrogen treatment. As the usage time of these catalysts increases, sulfur and carbon content, which are impurities in petroleum, adhere to the surface of these catalysts, and their catalytic activity decreases.Therefore, catalysts whose activity has decreased to some extent may regain their activity. Therefore, regeneration processing is required. This catalyst regeneration treatment method consists of in-device regeneration, which is carried out while the catalyst remains in the reactor, and out-of-device regeneration, which is carried out by extracting the spent catalyst whose activity has decreased from the reactor and using a dedicated regenerator. Broadly classified.

Although the in-device regeneration method saves the effort of extracting the catalyst, it takes time to regenerate, the reactor filled with the catalyst cannot be used during the regeneration process, and appropriate sampling means are not provided. On the other hand, external playback is expensive but takes less time because it uses a dedicated playback device. Furthermore, the reproduction state can be precisely controlled by the attached sampling means.

Therefore, conventionally, various catalyst regeneration devices for external regeneration have been proposed.

For example, according to Japanese Unexamined Patent Publication No. 59-213444, by using a vibrating conveyor or a rotary furnace, the waste catalyst is continuously moved inside a long and narrow chamber, and the waste catalyst is heated by electromagnetic waves. A method for activating, reactivating or regenerating a solid catalyst and an apparatus therefor are disclosed. Also, according to Japanese Patent Application Laid-Open No. 60-48149,
A spiral passage is formed in the inner circumferential wall of the rotary kiln made of porous metal in a direction that applies a conveying force from one end to the other end by rotation thereof, and the inside of the rotary kiln is defined into a plurality of chambers. A catalyst regeneration device is disclosed in which a processing gas passage is connected to the outside of the rotary kiln and is provided in each chamber through which processing gas passes through the wall of the rotary kiln. Furthermore, JP-A-60-9
According to Publication No. 4145, a continuous catalyst regeneration method is disclosed in which carbon and sulfur compounds in a waste catalyst are burned and removed in stages while controlling the oxygen content in the processing gas and the processing temperature, and an apparatus for this purpose is disclosed. A rotating tray, rotating conveyor or belt conveyor is used to move the catalyst.

[Problem to be Solved by the Invention 1] According to the conventional catalyst regeneration method and apparatus disclosed in JP-A-59-213444, etc., a vibrating conveyor, a rotary kiln, and a rotary tray are used to transfer the waste catalyst in the regenerator. etc., the device becomes complicated and the operating cost increases.

An object of the present invention is to provide a catalyst regeneration method and apparatus that can be carried out efficiently.

[Means for Solving the Problems] The method for regenerating a catalyst according to the present invention includes lowering the spent catalyst by gravity through a porous flow section in a first processing chamber, and flowing a processing gas into the first processing chamber. removing oil by passing the waste catalyst across the porous flow section; lowering the waste catalyst by gravity through the porous flow section of a second processing chamber that is continuous with the first processing chamber; a step of removing sulfur by passing the processing gas across the porous flow section while flowing it into the processing chamber; and a porous flow section of a third processing chamber that connects the waste catalyst with the second processing chamber. The inside is lowered by gravity,
The third processing chamber is characterized by a step of removing carbon by passing the processing gas across the porous flow section while flowing the processing gas into the third processing chamber.

In this catalyst regeneration method, the temperature of the processing gas introduced into the first processing chamber is preferably 200 to 380°C, and the oxygen concentration is 3% or less. If the temperature is less than 200°C, oil removal is difficult. If the temperature is insufficient and the temperature exceeds 380°C, there is a risk of ignition. Moreover, if the oxygen concentration exceeds 3%, it becomes easy to ignite. The processing gas introduced into the second processing chamber should preferably have a temperature of 300 to 450°C and an oxygen concentration of 1.0 to 5.0%. If the temperature is less than 300"C, the sulfur content will be removed by combustion. If the oxygen concentration exceeds 450°C, it will be heated more than necessary.Also, if the oxygen concentration is less than 1.0%, it will be difficult to burn, and if it is more than 5.0%, it will burn too much and the room will become overheated. The processing gas introduced into the third processing chamber should preferably have a temperature of 350 to 600°C and an oxygen concentration of 2.0 to 10%.
If the temperature is less than 50 degrees, combustion and removal of carbon will be insufficient, and 6
When the temperature exceeds 00'C, the catalyst activity decreases. When the oxygen concentration is lower than 2.0%, carbon becomes difficult to burn, and 10%
．． If it is more concentrated than 0%, it will burn too much and the temperature inside the room will become excessively high.

In this catalyst regeneration method, in addition to the catalyst regeneration process in the first to third processing chambers, the spent catalyst is passed by gravity through a porous flow section in a fourth processing chamber that is continuous with the third processing chamber. A step may be provided in which the remaining carbon content is completely removed by lowering the processing gas and passing it across the porous flow section while flowing the processing gas into the fourth processing chamber.

At this time, it is preferable that the processing gas introduced into the fourth processing chamber has a temperature of 450 to 600°C and an oxygen concentration of 3.0 to 10.0%. Since this treatment is for a case where carbon content is insufficiently removed in the third treatment chamber, the temperature and oxygen concentration must be higher than at least the temperature and oxygen concentration in the third treatment chamber.

In addition, the regeneration device for carrying out this catalyst regeneration method consists of a first treatment chamber for removing oil from the spent catalyst, a second treatment chamber for removing sulfur, and a third treatment chamber for removing carbon. A porous flow section through which the waste catalyst descends and a processing gas flow section are provided in each processing chamber. The provision of an inlet and a processing gas outlet is considered to be vf.

In this catalyst regeneration device, a fourth processing chamber for further removing carbon content can be provided after the third processing chamber and connected in the vertical direction.

[Example] An example of a catalyst regeneration device according to the present invention will be described with reference to the drawings. Note that the waste catalyst regenerated here is one that has been used for hydrogen treatment in an oil refinery plant.

This catalyst regeneration device includes a catalyst regeneration tower 10, a treated gas supply mechanism 70, and a treated gas discharge mechanism 90.

The catalyst regeneration tower 10 includes, in order from the top, a first processing chamber 11 for removing oil from the spent catalyst i, a second processing chamber 12 for removing sulfur, and third and fourth processing chambers for removing carbon. 13.
A hopper 15 for supplying the waste catalyst 1 is provided in the upper part of the first processing chamber 11 via a valve 14, and a valve 58 is provided in the lower part of the fourth processing chamber 35. A receiving portion 16 for the regenerated catalyst 2 is provided via the .

A porous screen 17 made of wire mesh or the like is attached to the hopper 15 along its conical inner circumferential surface.
This will remove some of the oil adhering to the The oil removed here is discharged through a waste oil line 18 connected to a hopper 17.

As shown in FIGS. 3 to 5, the upper connector 19 of the first processing chamber 11 is formed into a flat rectangular cylindrical shape with an upper surface plate 19A joined to the upper surface of the first processing chamber 11 via a gasket 19D. The connecting part 19B on the valve 14 side forms a falling flow path for the waste catalyst 1, and the locking part 19C is fitted with the upper end of the porous flow part 21 of the first processing chamber 11, which will be described later. Ru.

As shown in FIGS. 6 to 8, the first processing chamber 11 for removing oil is provided with a cylindrical body 20 and in the center of this body 20 in the vertical direction, and is located inside the spent catalyst 1. A porous circulation section 21 that constitutes a falling passage, and this porous circulation section 21
Two gas flow portions 22A are formed within the cylindrical body 20 by partitioning the two gas flow portions 22A.

22B, and a heat insulating member 23 provided so as to cover the outer periphery of this cylindrical body 20.

This cylindrical body 20 has an inlet 24 for introducing the processing gas 3 on one side of the gas circulation section 22A, and an outlet 25 for discharging the processing gas 3 on the other side of the gas circulation section 22B. It is formed.

Note that these inlet ports 24 and outlet ports 25 are shown as 1 in the figure.
However, by branching the processing gas supply line within or near the cylinder body 20, the process gas supply line is formed at a plurality of positions, for example, three positions, with respect to the cylinder body 20. An oil pan 26 is provided at the bottom of the cylindrical body 20 to collect the oil contained in the removed waste catalyst l. An oil drain port 26A connected to the line 34 is formed.

As shown in FIGS. 9 to 11, the porous flow section 21 includes a pair of rectangular frame members 27 and a lattice-shaped frame member 28 with a porous screen 29 sandwiched between them, and a cylindrical body 20. It is attached by a holder 31 at a predetermined interval via a positioning member 30 fixed to the inner surface of the upper connector 19, and its upper end is configured to fit into the locking portion 19c of the upper connector 19.

These frame members 27 and 28 are rectangular frames in consideration of the fact that the pressure of the waste catalyst 1 is applied from the inside of the porous flow part 21 to the gas flow parts 22A and 22B side when the waste catalyst l is lowered. The member 27 is arranged on the side of the porous flow section 21, and the lattice-shaped frame member 28 is arranged on the side of the gas flow sections 22A and 22B. Further, when the positioning member 30 is hollow, a shielding plate 30A is attached to the upper surface of the positioning member 30 in order to prevent the spent catalyst 1 from entering the inside. Note that this porous screen 29 is made of, for example, a 16-mesh wire mesh using a wire rod having a diameter of 0.635 m.

As shown in FIG. 7, the first processing chamber 11 is equipped with a thermometer 32 for monitoring internal temperature and a nozzle 33 for sampling the waste catalyst 1 at its lower part. At this time, the nozzle 33 has its inner end opened at an angle of about 45 degrees diagonally upward toward the center of the cylindrical body 20, and samples a predetermined amount of the waste catalyst l falling by gravity within the porous flow section 21 from the internal opening. It is now possible to do so.

As shown in FIGS. 12 to 14, the partition plate 31 provided between the first processing chamber 11 and the second processing chamber 12 is engaged with the lower end of the porous flow section 21 of the first processing chamber 11. Locking part 31
A is formed in the upper part, and a locking part 31B to which the porous flow part 37 of the second processing chamber 12 is locked is formed in the lower part. This partition plate 31 has an end 31C with a gasket 31D between the lower flange 2OA of the cylinder 20 of the first processing chamber 11 and the upper flange 36A of the cylinder 36 of the second processing chamber 12. It is joined through.

The second processing chamber 12 for removing sulfur content includes the 15th to 1st processing chambers.
As shown in FIG. 7, it has the same configuration as the first processing chamber 11 described above, and includes a cylindrical body 36 and a porous flow section 37 inside the cylindrical body 36.
It has two gas flow parts 38A and 38B, and is further provided with a heat insulating member 39 that covers the outer periphery of the cylinder body 36.

In the case of this cylindrical body 36 as well, an inlet 40 for introducing the processing gas 3 is formed on one side of the gas circulation section 3BA, and an outlet for discharging the processing gas 3 on the other side of the gas circulation section 38B. 41 is formed. Note that, similarly to the cylinder body 20 of the first processing chamber 11, these inlet ports 40 and discharge ports 41 are formed at a plurality of locations, for example, three locations, with respect to the cylinder body 36.

The porous flow section 37 provided in the second processing chamber I2 is similar to the porous flow section 21 provided in the first processing chamber 11.
A frame member 37A having the same configuration as that, that is, a square and grid-like frame member
, 37B, and a porous screen 37C interposed between them.

This second processing chamber 12 also has a thermometer 42 for monitoring the internal temperature and a nozzle 43 for sampling the waste catalyst 1 at its lower part.
is attached.

A partition plate 44 (see Fig. 1.2) provided between the second processing chamber 12 and the third processing chamber 13 is used to separate the first processing chamber 11 and the second processing chamber 12 shown in Figs. It has the same configuration as the partition plate 31 provided therebetween.

The third processing chamber 13 for removing carbon content includes the 18th to 2nd processing chambers.
As shown in Figure 0, the above-mentioned first and second processing chambers 11 and 12
It has a structure similar to that of the cylinder body 47, and has a porous circulation part 48 and two gas circulation parts 49A and 49B in the cylinder body 47, and further includes a heat insulating member 50 that covers the outer periphery of the cylinder body 47. ing. In addition, since the fourth processing chamber 35 has exactly the same configuration as the third processing chamber 13, the same reference numerals as those used in the third processing chamber 13 will be used, and the fourth processing chamber 35 will also be described. do.

This cylindrical body 47, as in the case of the second processing chamber 12,
An introduction port 51 for introducing the processing gas 3 is formed on one gas distribution section 49A side, and the other gas distribution section 49B
A discharge port 52 for discharging the processing gas 3 is formed on the side. Note that these inlet ports 51 and outlet ports 52 are also formed at a plurality of locations, for example, three locations, with respect to the cylindrical body 47.

The porous flow section 4B provided in the third processing chamber 13 has the same configuration as the porous flow section 21.37 provided in the first and second processing chambers 11.12, that is, a square shape and a lattice shape. It has a pair of frame bodies consisting of frame members 48A, 48B and a porous screen 48C interposed between them.

This third processing chamber 13 also has a thermometer 53 for monitoring the internal temperature and a nozzle 54 for sampling the waste catalyst 1 at its lower part.
is attached.

As shown in FIGS. 21 to 23, the lower connector 57 of the third processing chamber 13 is connected to the lower surface of the second processing chamber 13 (gas care) 57D.
The bottom plate 57A is joined via the bottom plate 57A.

It is composed of a connecting portion 57B with the porous flow section 48 and a connecting portion 57C with the valve 58.

A receiving portion 16 for the regenerated catalyst 2 is connected to the bottom of the third processing chamber 13 via a valve 58 . Note that as the valve 14.58, a ball valve with a limit switch, a slide valve, or a row feeder can be used. Inside this receiving part 16, a water-cooled coil pipe 59 (a first
(see figure) is installed.

Note that, as shown in FIG. 2, the catalyst regeneration tower 10 is fixed to a frame (not shown) or the like via a stay 60.

The processing gas supply mechanism 70 has a high temperature processing gas supply line 71 as its main line, as shown in 111F.
A first branch line 71A that branches from this processing gas supply line 71 and communicates with the first processing chamber 11, and a second processing chamber 1.
2, the second branch line 71B communicates with the third and fourth processing chambers 13.35, and the third branch line communicates with the third and fourth processing chambers 13.35? It has an IC.

A high-temperature process gas supply line 71 is led from an incinerator 73 connected as a downstream part of an existing flue gas treatment device 72 in a petrochemical plant, etc., and a blower 74 as a forced air supply means is provided in the middle of the incinerator 73. .

The first branch line 71A communicating with the first processing chamber 11 is provided with an air-cooled cooling means 75 consisting of a large number of bare tubes in order to lower the temperature of the processing gas. Note that this cooling can also be performed in combination with a water-cooled cooling means 76 that showers the bare tube of the cooling means 75 with water.

In the case of the second branch line 71B communicating with the second processing chamber 12, a temperature adjustment line 77 that guides an appropriate amount of the processing gas cooled by the cooling means 75 of the first branch line 71A as needed is led from the first branch line 71A. It's dark. That is, in the second branch line 71B, a gas whose temperature is adjusted by mixing the high temperature gas from the processing gas supply line 71 and the cooled gas from the first branch line 71A flows.

A third branch line 71C communicating with the third and fourth processing chambers 13.35 is directly connected to the processing gas supply inlet 71 so that the high temperature gas from the processing gas supply line 71 flows.

Air supply valves 18 and 19 are installed in the middle of the second branch line 71B and the third branch line 71C, respectively, for adjusting the oxygen concentration in the processing gas. Further, sampling valves 80, 81. are provided in the middle of the processing gas supply line 71, the second branch line 71B, and the third branch line 71C, respectively, for measuring the oxygen concentration in the processing gas.
82 is provided, and is connected to an oxygen concentration measuring device (not shown) via these valves 80, 81, and 82.

In addition, as shown in the figure, each line 71.71A.

At appropriate positions of 71B and 71C, on-off valves V and flow i
A t%A regulating valve C, a flow meter F, a pressure gauge P, and a thermometer T are provided. Moreover, a waste heat boiler 83 and a chimney 84 are further attached to the latter stage of the incineration tJ313. Furthermore, although not shown, the processing gas supply lines 7LA, TIB,'
? Accident prevention means such as fire using steam or nitrogen are provided at appropriate locations on the IC. Further, the hopper 15 is also provided with an accident prevention means using nitrogen.

The processing gas discharge mechanism 90 includes a first discharge line 91 connected to the gas discharge port 25 of the first processing chamber 11 and a second discharge line 92 connected to the gas discharge port 41 of the second processing chamber 12.
A, a third exhaust line 92B connected to the gas exhaust ports 52 of the third and fourth processing chambers 12.35 is provided.

A gas-liquid separator 93 is installed in the middle of the 10F output line 91 to separate oil from the waste gas, but even after the oil has been separated, the waste gas still contains some oil. The gas is returned to the inlet side of the incinerator 73, where it is incinerated together with other combustible gases. On the other hand, the oil separated by the gas-liquid separator 93 passes through an oil drain line 94 and is stored in a container 95. The third discharge line 92B has an air supply valve 78.7 in the middle thereof.
A heat exchanger 96 connected to 9 is provided, by means of which the inlet air is preheated. And this line 92B is
The exhaust line 92 is integrated with the second exhaust line 92A, and is returned to the inlet side of the waste heat boiler 83, and the incinerator 73
The waste heat boiler 83 heats water together with high-temperature combustion gas from the waste heat boiler 83. At this time, a bypass line 7ID is connected in the middle of the discharge line 92, and in order to ensure the flow rate on the exhaust side of the blower 74 at a predetermined amount (minimum flow) when the blower 74 is started up, this bypass line 71D supplies the processing gas. It is connected to line 71.

Next, a method for regenerating a catalyst using this regenerator will be explained.

First, the spent catalyst 1 used for hydrogen treatment in a petroleum refinery plant is charged into the hopper 15 of the catalyst regeneration tower IO.

Next, by adjusting the opening degrees of the upper and lower valves 14, 58 of the catalyst regeneration tower 10, the spent catalyst lO is discharged into the catalyst regeneration tower 10.
control the amount of introduction. The spent catalyst 1 descends by gravity through the valve 14 and is introduced into the first processing chamber 11.

At this time, a processing gas supply line 7 is provided in the first processing chamber II.
A processing gas 3 having a temperature of 250° C. and an oxygen concentration of 0.2 to 0.3% is supplied from an inlet 24 of the cylindrical body 20 via the first branch line 71A and the first branch line 71A. In this first processing chamber 11, the processing gas 3 is supplied to one processing gas distribution section 2.
By passing from 2A across the porous flow section 21 and going to the other treated gas flow section 22B, it comes into contact with the waste catalyst 1 that is descending inside the porous flow section 21, and the oil content of this waste catalyst 1 is removed. Remove. The removed oil is collected in the oil pan 26 at the bottom of the cylindrical body 20 and is discharged through the oil drain line 34.

The processing gas 3 that has passed through the porous flow section 21 is discharged through the exhaust port 25.
It passes through the gas-liquid separator 93 and is returned to the incinerator 73, where some of the oil contained therein is burned off. Note that the state of oil removal in the first processing chamber 11 is constantly monitored by an attached sampling nozzle 33. Further, the temperature inside the porous flow section 21 is detected by the thermometer 32, and the temperature of the first discharge line 91 is also detected by the thermometer T, and based on these temperatures, the fluid is discharged from the first branch line 71A. The temperature of the processing gas 3 is adjusted.

Next, the spent catalyst 1 from which oil has been removed in the first processing chamber 11 continuously descends by gravity through the porous flow section 37 in the second processing chamber 12 . At this time, the second processing chamber 12 contains gas from the processing gas supply line 71 and the temperature 11-node line 7.
The processing gas 3 is mixed with the gas from 7 and brought to a temperature iP1 of 400°C, and is further supplied with oxygen via the air supply valve 78 to have an oxygen concentration of 2.2%.
It is supplied from 0. In this second processing chamber 12,
Processing gas 3 passes from one processing gas distribution section 38A across the porous distribution section 37 and goes to the other processing gas distribution section 38B, so that it is combined with the waste catalyst 1 that is descending inside the porous distribution section 37. The sulfur content of the spent catalyst 1 is removed by combustion. The processing gas 3 that has passed through the porous flow section 37 is returned to the waste heat boiler 83 from the exhaust port 41 through the exhaust lines 92A and 92. Note that the state of sulfur removal in the second processing chamber 12 is constantly monitored by an attached sampling nozzle 43. In addition, in this second processing chamber 12, as in the first processing chamber 11, a second branch is established based on the temperature detected by the thermometer 42 in the porous flow section 37 and the thermometer T in the second discharge line 92A. The processing gas temperature and oxygen concentration in line 71B are adjusted.

Next, the spent catalyst 1 from which the sulfur content has been removed in the second processing chamber 12
continuously descends by gravity through the porous flow section 48 in the third processing chamber 13. At this time, in the third processing chamber 13,
Processing gas having a temperature of 450° C. and an oxygen concentration of 3.3% is supplied from the inlet 51 of the cylinder 47 via the third branch line 71C and the air supply valve 79.

In this third processing chamber 13, the processing gas 3 passes from one processing gas distribution section 49A across the porous distribution section 4 and goes to the other processing gas distribution section 49B. Contact with the descending spent catalyst 1 within 4 days,
The carbon content of this waste catalyst 1 is removed by combustion. Porous flow section 4
The processing gas 3 that has passed through the exhaust port 8 passes through the third exhaust line 92B from the exhaust port 52, and is heated to a high temperature due to combustion, so it is cooled in the heat exchanger 96 and returned to the waste heat boiler 83. At this time, in the heat exchanger 96, the air heated to high temperature by exchanging heat with the process gas 3 in the third discharge line 92B is transferred to the second
The air is supplied to the air supply valves 78 and 79 provided in the third branch lines 71B and 71C, so as not to lower the processing gas temperature in these second and third branch lines 71B and 71C. ing.

Note that the state of carbon removal in the third processing chamber 13 is also monitored at any time by the attached sampling nozzle 54. Also, in the third processing chamber 13, the processing gas temperature and oxygen concentration in the third branch line 71C are adjusted based on the measurement results by the thermometer 53 and the like.

If the sampling nozzle 54 attached to the third processing chamber 13 monitors that the removal of carbon content in the third processing chamber 13 is insufficient, the sampling nozzle 54 connected to the third processing chamber 13 In the fourth processing chamber 35, a processing gas 3 having a higher temperature and higher oxygen concentration than the processing gas 3 supplied to the third processing chamber 13 is supplied, and carbon content is completely removed.

That is, this fourth processing chamber 35 has a temperature of, for example, 500''C.
A processing gas 3 having an oxygen concentration of 465% is supplied.

In this way, the first, second, third and fourth processing chambers 11.1
The waste catalyst 1 that has passed through the valve 2, 13, and 35 is regenerated, and the regenerated catalyst 2 is stored in the receiving portion 16 through the valve 58. Thereafter, when the regenerated catalyst 2 in the receiving part 16 reaches a predetermined amount, the slide valve 61 is opened and the regenerated catalyst 2 is transferred to a container 62 such as a drum can.

Thereafter, by continuing the above-described operations, the spent catalyst 1 is sequentially regenerated.

According to the catalyst regeneration method and apparatus according to the present example,
The catalyst regeneration tower 10 includes, from the top, a first processing chamber 11 that removes oil from the spent catalyst 1 and a second processing chamber 1 that removes the sulfur content.
2, and the third and fourth processing chambers 13.35 for removing carbon content.
Since these are vertically connected, the spent catalyst 1 naturally falls from the hopper 15 to the receiving part 16 by gravity, and no special transport means or energy is required. This is advantageous in that it can simplify the process and reduce operating costs.

In addition, since the waste catalyst 1 descends in the porous flow parts 21, 37.48 that are isolated from the cylinder 20, 36, 47, even if the cylinder goes out of control due to excessive supply of oxygen, 20.
36.47 is protected.

Since the fourth processing chamber 35 is further provided after the third processing chamber 13 for removing carbon, it is possible to completely remove carbon.

Although it is a natural descent method due to gravity, the flow rate of the spent catalyst 1 can be controlled by adjusting the opening degrees of the valve 14 under the hopper 15 and the valve 58 under the fourth processing chamber 35.

Since sampling nozzles 33, 43.54 are installed in each processing chamber 11, 12, 13.35, respectively, the processing status of the waste catalyst 1 in each processing chamber 11, 12, 13.35 can be accurately grasped. A regenerated catalyst with uniform quality can be obtained.

Furthermore, since the existing flue gas treatment device 72 is used as the supply source of the processing gas 3, there is no need to provide a dedicated supply device for the processing gas 3, which is economical.

Note that the present invention is not limited to the above embodiments,
Modifications within the scope of achieving the object of the present invention are included in the present invention.

For example, the configuration of the porous flow portions 21.37.48 of each processing chamber 11, 12.13.35 is arbitrary, and more specifically, as long as the screen 29 itself has sufficient strength, the frame It is also possible to construct the device without the elements 27,28. In addition, the screen 29 is not limited to a wire mesh, but may be a punched metal or other perforated plate.
Any porous member that can prevent escape from 1°37.48° is sufficient.

Further, the connection order of the second processing chamber 12 for removing sulfur content and the third and fourth processing chambers 13.35 for removing carbon content is arbitrary. Therefore, the second processing chamber 12 does not necessarily need to be located first, but the third and fourth processing chambers 13.35 may be located first, and the second processing chamber 12 may be located next. You may.

Although the third and fourth processing chambers 13.35 are provided as processing chambers for removing carbon, only one processing chamber may be provided depending on the waste catalyst I to be processed.

Furthermore, it goes without saying that the shape, structure, material, etc. other than these can be changed as necessary.

[Effects of the Invention] According to the present invention, since the catalyst can be regenerated efficiently, there is an effect that the equipment cost and operating cost can be reduced.

[Brief explanation of drawings]

The figures show one embodiment of the present invention, in which Fig. 1 is a schematic configuration diagram of a catalyst regeneration device according to this embodiment, Fig. 2 is a front view of a regeneration tower, and Fig. 3 is a plan view of an upper connector. , Fig. 4 is a side view thereof, Fig. 5 is a sectional view thereof, Fig. 6 is a plan view of the first processing chamber, Figs. 7 and 8 are sectional views thereof, and Fig. 9 is a plane view of the main parts. , 1O and 11 are front views of each frame member, and 12.
The figure is a plan view of the partition plate, FIGS. 13 and 14 are sectional views thereof, FIG. 15 is a plan view of the second processing chamber, and FIGS. 16 and 1.
7 is a sectional view thereof, FIG. 18 is a plan view of the third processing chamber, FIGS. 19 and 20 are sectional views thereof, FIG. 21 is a plan view of the lower connector, and FIGS. 22 and 23 are FIG. DESCRIPTION OF SYMBOLS 1... Spent catalyst, 2... Regenerated catalyst, 3... Processing gas, lO... Catalyst regeneration tower, 11... First processing chamber, 12
...Second processing chamber, 13...Third processing chamber, 35...
Fourth processing chamber, 20.36.47...Cylinder, 21,37
．． 48... Porous flow section, 22A, 22B, 38A,
38B. 49A, 49B... Gas distribution section, 24, 40.51.
...Gas inlet, js, 41.52...Gas outlet,
70... Processing gas supply mechanism, 90... Processing gas discharge mechanism. Applicant Softard Kogyo Co., Ltd. Kashima Engineering Co., Ltd. Tamade 8 Agent Patent attorney Sanzo Kinoshita (and 2 others) Figure 2 Figure 3 Figure 5 Figure 6 Figure 2 Otsu Figure 7 Figure 8 Figure 9 Figure 1O Figure 11 Figure 12 Figure 13 Figure 14 Figure 15 Figure 18 Figure 19 Figure 20 Figure 21 Procedural amendment (August 9, 1990 Hat Review No. 1-116938 2, Invention Name Catalyst regeneration method and equipment Address a=187 1-17-7 Misono-cho, Kodaira-shi, Tokyo
Name: Softard Kogyo Co., Ltd. Owner: Katsuhiko (1 person x 2 people) 4. Agent address: 4F Takagi Building, 1-7 Okubo-chome, Shinjuku-ku, Tokyo, 169 @ Tongue (03) 205-84718, revised Contents (1) In the specification, page 17, lines 5, 6, and 10, "Third processing chamber 13J" is corrected to "Fourth processing chamber 35." (2) Same, page 19, lines 7 to 10 [directly connected to the third and fourth processing chambers 13.35]. J to 1
Correct as shown below. [The third branch line that communicates with the third and fourth processing chambers 13.35? Similar to the second branch line TIB, the IC is connected to high temperature gas from the processing gas supply line 71 and the first branch line 7.
Temperature-controlled gas flows by mixing with the cooled gas from 1A. ” (3) Same, page 20, line 15 r2, 35J as “3°35
” he corrected. (4) Same, page 21, line 4, "air supply valve" is corrected to "air supply valve on the low temperature fluid side". (5)Amend Figure 1 in the drawings as shown in the attached sheet. that's all

Claims (6)

[Claims] (1) The spent catalyst is lowered by gravity through the porous flow section in the first processing chamber, and while flowing the processing gas into the first processing chamber,
removing oil by passing the waste catalyst across the porous flow section; lowering the spent catalyst by gravity through the porous flow section of a second processing chamber that is continuous with the first processing chamber; a step of removing sulfur by passing the processing gas across the porous flow section while flowing it into the processing chamber; and a porous flow section of a third processing chamber that connects the waste catalyst with the second processing chamber. A method for regenerating a catalyst, comprising the step of lowering the catalyst by gravity, and removing carbon by passing the processing gas across the porous flow section while flowing the processing gas into the third processing chamber. . (2) In the catalyst regeneration method according to the first claim, the processing gas introduced into the first processing chamber has a temperature of 200 to 3
The processing gas is introduced into the second processing chamber at a temperature of 80°C and an oxygen concentration of 3% or less, and the processing gas is introduced into the third processing chamber at a temperature of 300 to 450°C and an oxygen concentration of 1.0 to 5.0%. The processing gas has a temperature of 350
A method for regenerating a catalyst, characterized in that the temperature is 600°C and the oxygen concentration is 2.0 to 10.0%. (3) In the method for regenerating a catalyst according to claim 1, in addition to the step of regenerating the catalyst in the first to third processing chambers, the spent catalyst is transferred to a fourth processing chamber that is continuous with the third processing chamber. It is characterized by providing a step of completely removing residual carbon by lowering the gas through the porous flow section by gravity and passing it across the porous flow section while flowing the processing gas into the fourth processing chamber. A method for regenerating a catalyst. (4) In the method for regenerating a catalyst according to claim 3, the processing gas introduced into the fourth processing chamber has a temperature of 450 to 6
A method for regenerating a catalyst, characterized in that the temperature is 00°C and the oxygen concentration is 3.0 to 10.0%. (5) A first treatment chamber for removing oil from the spent catalyst, a second treatment chamber for removing sulfur, and a third treatment chamber for removing carbon are vertically connected, and each treatment chamber In addition to providing a porous flow section through which the waste catalyst descends and a processing gas flow section,
A catalyst regeneration device characterized in that each processing chamber is provided with a processing gas inlet and a processing gas outlet so that the processing gas crosses the porous flow section. (6) The catalyst regeneration apparatus according to claim 5, characterized in that a fourth processing chamber for further removing carbon content is provided after the third processing chamber and connected in a vertical direction. Device.