KR101250173B1 - Magnetic separation method of fluidized catalytic cracking catalyst - Google Patents

Abstract

In the magnetic separation device of a fluid catalytic cracking catalyst, there is provided a method of reducing the waste of the equilibrium catalyst by increasing the amount of catalyst used for regeneration by improving the separation efficiency. In a fluid catalytic cracking process having a magnetic separator, magnetic separation of the fluid catalytic cracking catalyst is introduced into a magnetic separator after adjusting the amount of water of the catalyst extracted from the fluid catalytic cracking apparatus to 5 mass% or less. Way.

Fluid catalytic cracking catalyst, magnetic separation method, equilibrium catalyst, magnetic separator, moisture content

Description

MAGNETIC SEPARATION METHOD OF FLUIDIZED CATALYTIC CRACKING CATALYST}

The present invention relates to a magnetic separation method of a catalyst extracted from a fluid catalytic cracking device in a fluid catalytic cracking process of heavy petroleum oil having a magnetic separator.

Fluid catalytic cracking is a method of decomposing petroleum hydrocarbons by contact with a catalyst to obtain products such as gasoline, liquefied petroleum gas, alkylated raw materials, and intermediate residual mixtures.

Recently, due to environmental problems or ease of use, the demand for hydrocarbon oils having boiling residues below light oil is relatively increasing, and converting heavy oil into soft oil by any method has become an important problem. In the meantime, the importance of fluid catalytic cracking which uses heavy petroleum as a raw material as a heavy oil processing process is increasing.

In the case of performing fluid catalytic cracking of heavy petroleum, a phenomenon in which metals such as nickel, vanadium, iron, copper, etc. contained in the crude oil are deposited on the catalyst is particularly remarkable. These metals are derived from contact with crude oil or transportation storage and processing equipment, and are generally present as organometallic compounds based on the porphyrin ring structure. Will be.

Such metals not only lower the activity of the catalyst but also lower the selectivity of the catalyst. That is, these metals have hydrogenation and dehydrogenation capability, and promote the dehydrogenation of hydrocarbons under the reaction conditions of fluid catalytic cracking, and as a result, the amount of hydrogen gas or coke that is undesirable as a product increases, and the preferred liquefied petroleum oil. Gas, gasoline and kerosene production are reduced.

In order to avoid such lowering of catalytic activity or deterioration of selectivity, in the fluid catalytic cracking of heavy oil or residual oil containing a large amount of metal, a part of the catalyst in the circulation system is usually periodically or normally extracted and exchanged with a new catalyst to keep the activity constant. Although the method is employ | adopted, it is necessary to remarkably increase the extraction amount of a catalyst, and high cost is especially required. In addition, the disposal of the extracted catalyst (hereinafter referred to as the equilibrium catalyst) is an industrial waste, which results in an additional cost for the treatment.

The catalyst usually has a particle diameter of 30 µm to 150 µm, but its strength decreases by being used for the reaction in the apparatus, and the particle diameter becomes smaller as the catalyst having a longer holding time in the apparatus. As a result, the catalyst having a long distribution time in the device has a large proportion of the catalyst having a very small particle diameter having a particle diameter of 30 µm or less, and thus the loss of the catalyst or the C heavy oil in the device by scattering or mixing into undecomposed oil in the device. Problems such as the mixing of the catalyst into the middle have been caused. In addition, the catalyst particle diameter here is computed from the distribution of each particle diameter using nine types of filters from which a mesh size differs.

As a means to solve this problem, the equilibrium catalyst is a self-adhesive catalyst in which a large amount of metals such as nickel and vanadium contained in the heavy petroleum oil of the raw material oil are deposited and become a self-adhesive, and a non-magnetic self-adhesive due to the low deposition of metal. As a deposition catalyst, a method of separating using a magnetic separation device, regenerating a non-magnetic adhesion catalyst, and then returning it to a fluid catalytic cracking device is known (for example, JP 63-37835 and JP 63-37156). Publication).

It has been confirmed that the separation method of the catalyst using the magnetic separation device is an effective method. However, the magnetic adhesion catalyst which becomes a magnetic deposit by depositing a large amount of metals such as nickel and vanadium by using this method and the deposition of the metal has little magnetic adhesion. In the case of separation with a nonmagnetic attachment catalyst which is not used, the separation efficiency is not necessarily sufficient. Especially, considering that the catalytic cracking activity of the nonmagnetic attachment catalyst used for regeneration is inferior to that of the new catalyst, Since the amount of the self-adhesive catalyst cannot be increased, there is a problem in that the amount of equilibrium catalysts discarded cannot be reduced.

It is an object of the present invention to further reduce the separation efficiency of the equilibrium catalyst by further improving the separation efficiency in the magnetic separation device of the fluid catalytic cracking catalyst and, as a result, increasing the amount of catalyst used for regeneration. Furthermore, it aims at reducing the ratio of the catalyst of the extremely small particle diameter whose particle diameter is 30 micrometers or less in the catalyst used for regeneration by improving separation efficiency.

The present inventors conducted earnest research and found that in the fluid catalytic cracking process including the magnetic separator, when the catalyst extracted from the fluid catalytic cracking apparatus is magnetically separated, the equilibrium catalyst has a water content of 5% by mass or less, thereby It has been found that the separation efficiency is greatly improved, and the present invention has been completed.

That is, in the fluid catalytic cracking process including the magnetic separator, the present invention adjusts the water content of the catalyst extracted from the fluid catalytic cracking apparatus to 5 mass% or less, and then introduces the catalytic catalytic cracking catalyst into the magnetic separator. It relates to a magnetic separation method of.

Hereinafter, the present invention will be described in detail.

The method of the present invention is applied to a fluid catalytic cracking process having a magnetic separation device. In a general fluid catalytic cracking process having a magnetic separation device, first, heavy petroleum oil is decomposed by contacting with a catalyst held in a fluid state in a fluid catalytic cracking device, and then stripped of the decomposition product, unreacted raw material and the catalyst. Treatment removes most of the degradation products and unreacted products. The catalyst with carbonaceous and some heavy hydrocarbons attached is withdrawn from the stripping zone and then transferred to a magnetic separation device. In the magnetic separation apparatus, a large amount of metal is deposited to separate the magnetic adhesion catalyst which becomes a magnetic deposit, and the non-magnetic adhesion catalyst which is not magnetically adhered due to the small amount of metal deposition, and the nonmagnetic adhesion catalyst is transferred to the regeneration tower. The regeneration tower is subjected to oxidation treatment to reduce carbonaceous and heavy hydrocarbons attached to the catalyst. In such a regeneration tower, the catalyst is maintained in a flow state, and combustion is usually performed at 550 to 850 ° C by air. The catalyst subjected to this oxidation treatment is a regeneration catalyst, which is returned to the reaction zone of the fluid catalytic cracker.

The present invention adjusts the amount of the extracted catalyst to 5% by mass or less before transferring the catalyst extracted from the fluid catalytic cracker to the magnetic separation device, and then introduces the magnetic adhesion catalyst and the non-magnetic adhesion catalyst by introducing the catalyst into the magnetic separation device. The separation efficiency is significantly improved.

As heavy petroleum oil used as a raw material, heavy petroleum oil containing distillation residues, such as heavy metals, such as nickel and vanadium, and asphaltene, is used. Specifically, the atmospheric distillation residual oil of crude oil, the vacuum distillation residual oil, the thing which hydroprocessed these, the mixture thereof, etc. are mentioned.

As the method of contacting the raw material and the catalyst, a method such as that performed in a fluidized bed of the catalyst and a liner-cracking in which the catalyst particles and the raw material move the tube together may be employed, but the present invention is applied to any method. .

The reaction conditions of the fluid catalytic cracking device are not particularly limited, and ordinary reaction conditions may be employed. For example, a reaction temperature of 480 to 650 ° C., a pressure of 0.1 to 0.3 MPa, a catalyst / oil ratio of 1 to 20, and a contact time of 0.1 to 10 seconds may be used.

The catalyst should just be a catalyst normally used for catalytic cracking of petroleum, and there exist a zeolite type catalyst etc., for example. Moreover, the particle diameter of a catalyst is not specifically limited, either, Usually, 5-200 micrometers, Preferably it is 30-150 micrometers.

In the present invention, the water content of the catalyst (equilibrium catalyst) extracted from the fluid catalytic cracker is adjusted to 5% by mass or less and then introduced into the magnetic separation device. 3 mass% or less is more preferable, and 1 mass% or less is especially preferable. When the amount of moisture exceeds 5% by mass, when the temperature of the equilibrium catalyst decreases due to cooling, water vapor contained in the equilibrium catalyst aggregates and the catalyst particle weight of the equilibrium catalyst changes, so that the separation efficiency is deteriorated. The effect of is not obtained.

Moreover, in this invention, after adjusting the temperature of the equilibrium catalyst introduce | transduced into a magnetic separation apparatus to 100 degrees C or less, it is preferable to introduce into a magnetic separation apparatus. The temperature of the equilibrium catalyst is more preferably 80 ° C or lower, and particularly preferably 60 ° C or lower. If the temperature of the equilibrium catalyst is higher than 100 ° C, when the temperature of the equilibrium catalyst decreases due to cooling, water vapor contained in the equilibrium catalyst aggregates and the catalyst particle weight of the equilibrium catalyst changes, so that the separation efficiency may be deteriorated. have. Moreover, although there is no restriction | limiting in particular about a minimum temperature, 10 degreeC or more is preferable and 20 degreeC or more is more preferable.

The method of bringing the water content of the equilibrium catalyst to a predetermined ratio is not particularly limited, and any method may be used. For example, there is a method in which the moisture content is 5% by mass or less using Degussa. Degussa is a drum having fins for heat dissipation to the outside, and is a device for reducing the moisture and the equilibrium catalyst temperature contained in the equilibrium catalyst extracted from the fluid catalytic cracking device by sucking dry air therein. In addition, for the purpose of further cooling the temperature of the equilibrium catalyst, a cooler may be further provided.

In the present invention, by controlling the amount of water in the equilibrium catalyst introduced into the magnetic separation device, the separation efficiency in the magnetic separation device can be improved, thereby enabling an increase in the amount of catalyst used for regeneration, thereby reducing the waste of the equilibrium catalyst. .

In the present invention, the separation efficiency is a difference between the metal deposition amount, the specific surface area, Mean activity difference by micro activity test (MAT).

For example, the separation efficiency of nickel can be calculated by the ratio of the self-adhesive catalyst to be discarded and the non-magnetic adhering catalyst used for regeneration to the ratio of the self-adhesive material containing a large amount of nickel deposited on the catalyst particles and the non-magnetic adhering material. Therefore, the metal deposition amount of the nonmagnetic attachment / the metal deposition amount of the magnetic attachment, the value of 1.0 indicates the case where no separation occurs, and the smaller the value, the higher the separation efficiency.

In addition, the surface area here means BET specific surface area measured by the BET method. The larger the surface area, the greater the activity of the catalyst. Moreover, MAT here is a value defined by ASTM D-3907 (FLUID CRACKING CATALYST BY MICROACTIVITY TEST), and the larger this value, the higher the activity of the catalyst.

As described above, the catalyst extracted from the fluid catalytic cracker is delivered to the magnetic separator after the amount of water is adjusted to 5% by mass or less.

The magnetic separator is a magnetic separator capable of continuously separating the nickel, vanadium, iron and copper magnetic deposits deposited on the catalyst particles and the nonmagnetic deposits having a small metal deposition amount according to the difference in the magnetization rate thereof. Particularly preferred are high gradient magnetic separators.

The high gradient magnetic separator inserts ferromagnetic fillers into a uniform high magnetic space and generates a high magnetic gradient of 200 × 10 ³ to 20000 × 10 ³ gauss / cm 2 around the fillers, thereby producing ferromagnetic or A magnetic separator designed to magnetically adhere magnetic particles of paramagnetic microparticles and to separate them from weak paramagnetic particles or diamagnetic microparticles of nonmagnetic attachments. An example of a high gradient magnetic separator is HGMS manufactured and sold by Metso Minerals.

In addition, the weight ratio of the magnetic adhering substance to the nonmagnetic adhering substance is preferably in the range of 1: 9 to 9: 1, and more preferably in the range of 1: 9 to 5: 5.

Fills made of ferromagnetic materials are usually reticulated, and the material is not a problem if they are ferromagnetic materials. Examples thereof include expanded metals made of stainless steel.

The wire diameter of the network of the network filler is usually 10 to 1000 µm, preferably 50 to 700 µm. In addition, in order for the catalyst particles to be extracted through the packing, the netting of the packing is preferably in the range of 3 to 80 mesh, more preferably in the range of 5 to 50 mesh. If the mesh is larger than 80 mesh, the nonmagnetic attachment is also mechanically retained, and if it is smaller than 3 mesh, it is not preferable because the filling is more likely to pass out without self-adhesion efficiently. Although one or more network fillers are laminated and used, in some cases, spacers or the like may be inserted between the network fillers and spaced at regular intervals.

Magnetic separation is performed by passing the catalyst along with the conveying fluid into the magnetic space of the magnetic separator. The conveying fluid is not particularly limited so long as it does not adversely affect the catalyst, but in terms of economy and safety, air, nitrogen or a mixture thereof may be used.

Process variables when operating a high gradient magnetic separator include magnetic strength, magnetic gradient, particle concentration, conveying fluid linear velocity, etc., catalyst particle diameter, the type and condition of the deposited metal, the separation level for the purpose, separation efficiency, etc. The optimum value of the process variable therefore varies.

The magnetic strength is the strength of the magnetic field in the space in which the packing material is placed, and is usually 1000 gauss or more, preferably 3000 gauss or more.

The magnetic field gradient is an amount of change according to the distance of the magnetic field intensity generated around the packing material, and has a close relationship with the wire diameter of the network packing material. However, the smaller the wire diameter, the larger the magnetic field gradient becomes.

Particle concentration refers to the concentration of catalyst particles in the transfer fluid. Usually, 0.01 to 100 g / l, preferably 0.1 to 10 g / l.

In addition, the conveying fluid linear velocity is a linear velocity of the conveying fluid when passing through the magnetic field space, and the separation level and the separation efficiency can be greatly changed by changing the conveying fluid linear velocity. The conveying fluid linear velocity is usually 0.01 to 50 m / sec, preferably 0.1 to 10 m / sec. If the conveying fluid linear velocity is less than 0.01 m / sec, the non-magnetic deposit also stays mechanically, and if it is larger than 50 m / sec, most of the magnetic adsorbent will pass through and be discharged. not.

The non-magnetic adhesion catalyst separated from the magnetic separation device is transferred to the regeneration tower, and the magnetic adhesion catalyst is discarded. At this time, the same amount of new catalyst as that of the discarded catalyst is replenished from a place which does not interfere with the operation of the apparatus. In addition, in order to keep the activity of the catalyst circulating in the apparatus constant, a part of the catalyst may be extracted from a suitable place which does not interfere with the operation of the apparatus, and a new catalyst of the same amount may be replenished. In addition, the catalyst may be continuously discharged or may be discharged discontinuously at regular intervals within a range that does not adversely affect performance.

Example

Hereinafter, although an Example is given and this invention is demonstrated concretely, this invention is not limited to these Examples.

(Example 1)

After adjusting the moisture content of the extracted catalyst (equilibration catalyst) to 1 mass% and temperature to 30 degreeC, it separated-separated by the high gradient magnetic separator. In the high gradient magnetic separator, expanded metal made of stainless steel was used as the filling material, and air was used as the conveying fluid.

The extraction catalyst, the magnetic adsorbate, and the nonmagnetic adsorbate were subjected to metal analysis, surface area analysis and activity evaluation by MAT. These results are shown in Table 1.

As shown in Table 1, very good separation efficiency was obtained when magnetic separation was carried out by adjusting the water content of the equilibrium catalyst to 1% by mass and the temperature to 30 ° C. The amount of metal deposited on the nonmagnetic attachments returned to the apparatus for regeneration is very small compared to the equilibrium catalyst, and the surface area is large, so the MAT conversion rate is high, so that the separation efficiency in the magnetic separation device is improved, and thus the amount of catalyst used for regeneration. As a result of this increase, the waste volume of the equilibrium catalyst was greatly reduced.

In addition, compared to the equilibrium catalyst, since the ratio of the extremely small particle diameter catalyst having a particle diameter of 30 µm or less returned to the apparatus and used for regeneration is small, the catalyst in the apparatus generated by incorporation into the fugitive or non-degradable oil outside the apparatus Loss or incorporation of the catalyst into the C-heavy oil can be reduced.

Example 1 Equilibrium catalyst magnetism
detach
Condition Treatment temperature ℃
Moisture content mass%
Magnetic strength KGauss
Linear velocity m / sec
Catalyst particle concentration g / l
Separation Ratio 30
1.0
12.9
4.2
0.17
Magnetic Attachments: Nonmagnetic Attachments = 1: 4 Amount of metal Self-adhesive Nonmagnetic attachment Nickel Mass-ppm
Vanadium mass-ppm 4120
13730 1240
4110 1820
6040 Performance Surface area ㎡ / g
MAT conversion mass%
% Of particle diameter less than 30㎛ 67
35.5
0.91 149
76.6
0.16 133
69.4
0.31 Separation Efficiency Nickel
vanadium 0.301
0.299

(Examples 2 to 5)

The amount of water of the extracted catalyst (equilibrium catalyst) was changed to 2% by mass, 3% by mass, 4% by mass and 5% by mass and separated in a high gradient magnetic separator. In the high gradient magnetic separator, expanded metal made of stainless steel was used as a filler, and air was used as a conveying fluid. Metal analysis was performed on the extracted catalyst, magnetic adhering matter, and nonmagnetic adhering matter. The results are shown in Tables 2 to 5.

As shown in Tables 2 to 5, good separation occurs when the amount of water in the equilibrium catalyst is small. In other words, when the amount of water in the equilibrium catalyst is small, the amount of metal deposition of the nonmagnetic attachments returned to the apparatus and used for regeneration is extremely small compared to the equilibrium catalyst, thereby greatly reducing the waste of the equilibrium catalyst since the amount of catalyst used for regeneration is increased. Can be.

Example 2 Equilibrium catalyst magnetism
detach
Condition Treatment temperature ℃
Moisture content mass%
Magnetic strength KGauss
Linear velocity m / sec
Catalyst particle concentration g / l
Separation Ratio 100
2.0
12.9
4.2
0.17
Magnetic Attachments: Nonmagnetic Attachments = 1: 4 Amount of metal Self-adhesive Nonmagnetic attachment Nickel Mass-ppm
Vanadium mass-ppm 4080
13010 1270
4280 1820
6040 Separation Efficiency Nickel
vanadium 0.311
0.329

Example 3 Equilibrium catalyst magnetism
detach
Condition Treatment temperature ℃
Moisture content mass%
Magnetic strength KGauss
Linear velocity m / sec
Catalyst particle concentration g / l
Separation Ratio 100
3.0
12.9
4.2
0.17
Magnetic Attachments: Nonmagnetic Attachments = 1: 4 Amount of metal Self-adhesive Nonmagnetic attachment Nickel Mass-ppm
Vanadium mass-ppm 3870
12040 1320
4530 1820
6040 Separation Efficiency Nickel
vanadium 0.341
0.376

Example 4 Equilibrium catalyst magnetism
detach
Condition Treatment temperature ℃
Moisture content mass%
Magnetic strength KGauss
Linear velocity m / sec
Catalyst particle concentration g / l
Separation Ratio 30
4.0
12.9
4.2
0.17
Magnetic Attachments: Nonmagnetic Attachments = 1: 4 Amount of metal Self-adhesive Nonmagnetic attachment Nickel Mass-ppm
Vanadium mass-ppm 3450
10520 1420
4920 1820
6040 Separation Efficiency Nickel
vanadium 0.412
0.468

Example 5 Equilibrium catalyst magnetism
detach
Condition Treatment temperature ℃
Moisture content mass%
Magnetic strength KGauss
Linear velocity m / sec
Catalyst particle concentration g / l
Separation Ratio 30
5.0
12.9
4.2
0.17
Magnetic Attachments: Nonmagnetic Attachments = 1: 4 Amount of metal Self-adhesive Nonmagnetic attachment Nickel Mass-ppm
Vanadium mass-ppm 3010
9530 1510
5160 1820
6040 Separation Efficiency Nickel
vanadium 0.502
0.541

(Comparative Example 1)

Without adjusting the catalyst water content and the treatment temperature of the comparative example 1, it processed on the conditions which can isolate a magnetic adhering substance and a non-magnetic adhering substance in a high gradient magnetic separator. These results are shown in Table 6.

As shown in Table 6, when magnetic separation was carried out without adjusting the water content of the equilibrium catalyst, the separation efficiency as in Example 1 could not be obtained.

In addition, there is no change in the equilibrium catalyst and the catalyst ratio of the extremely small particle diameter whose particle diameter of the nonmagnetic attachment returned and used for regeneration is 30 µm or less, and the catalyst in the device caused by incorporation into the fly ash or undecomposed oil outside the device. The reduction effect such as loss of or incorporation of catalyst into C heavy oil was small.

Comparative Example 1 Equilibrium catalyst magnetism
detach
Condition Treatment temperature ℃
Moisture content mass%
Magnetic strength KGauss
Linear velocity m / sec
Catalyst particle concentration g / l
Separation Ratio 120
8.0
12.9
3.9
0.17
Magnetic Attachments: Nonmagnetic Attachments = 1: 4 Amount of metal Self-adhesive Nonmagnetic attachment Nickel Mass-ppm
Vanadium mass-ppm 2670
8880 1610
5330 1820
6040 Performance Surface area ㎡ / g
MAT conversion mass%
% Of particle diameter less than 30㎛ 110
47.5
0.52 139
75.1
0.26 133
69.4
0.31 Separation Efficiency Nickel
vanadium 0.603
0.600

(Comparative Example 2)

The treatment temperature was adjusted to 30 ° C. without adjusting the catalyst water content of Comparative Example 1, and the treatment was performed under conditions that could be separated into magnetic adhering materials and nonmagnetic adhering materials in a high gradient magnetic separator. These results are shown in Table 7.

As shown in Table 7, when the magnetic separation was carried out without adjusting the water content of the equilibrium catalyst, the separation efficiency as in Example 1 could not be obtained even by adjusting the treatment temperature.

Comparative Example 2 Equilibrium catalyst magnetism
detach
Condition Treatment temperature ℃
Moisture content mass%
Magnetic strength KGauss
Linear velocity m / sec
Catalyst particle concentration g / l
Separation Ratio 30
8.0
12.9
3.9
0.17
Magnetic Attachments: Nonmagnetic Attachments = 1: 4 Amount of metal Self-adhesive Nonmagnetic attachment Nickel Mass-ppm
Vanadium mass-ppm 2690
8900 1600
5320 1820
6040 Separation Efficiency Nickel
vanadium 0.595
0.598 69.4
0.31

(Comparative Example 6)

Catalytic cracking of atmospheric distillation residual oil is carried out by using a zeolite-based catalytic cracking catalyst, extracting a part of the circulating catalyst by a fluid catalytic cracking pilot device, and adding a supplemental amount of catalyst to maintain a constant amount of catalyst in the apparatus. did. In this case, 309 g of fresh catalyst per barrel of treated oil was required to obtain the product shown in Table 8.

Subsequently, the high contact magnetic separator was assembled and mounted on the fluid catalytic cracking pilot device, and the extracted catalyst was divided into a magnetic attachment and a nonmagnetic attachment using a high gradient magnetic separator under the same conditions as in Example 1, and the nonmagnetic attachment was returned to the circulation system. I used to play it. In this case, the amount of fresh catalyst required to obtain approximately the same product as without using high gradient magnetic separation was 210 g per barrel of treated oil. In this way, after adjusting the water content of the equilibrium catalyst, the separation treatment in the high gradient magnetic separator improves the separation efficiency of the magnetic adhering material and the nonmagnetic adhering material, thereby increasing the amount of catalyst used for regeneration. The amount of catalyst used and the amount of waste disposed of the equilibrium catalyst can be reduced.

No high gradient magnetic separator High Gradient Magnetic Separator Example 1 Conditions Comparative Example 1 Conditions Product distribution H ₂ mass%
C1 + C2 mass%
C3 + C4 mass%
Kaolin mass%
Circulating oil mass%
Coke Mass% 0.44
2.10
16.81
49.85
24.32
6.48 0.40
1.87
16.99
49.90
24.46
6.38 0.41
1.91
16.82
49.88
24.57
6.41 Equilibrium catalyst waste g / barrel 309 144 210

According to the method of the present invention, since the separation efficiency is remarkably improved in the magnetic separation device of the fluid catalytic cracking catalyst, the amount of catalyst used for regeneration can be increased, and the amount of discarded catalyst can be reduced.

In addition, since the catalyst having a large amount of metal deposition is a catalyst having a long holding time in the apparatus, there are many ratios of an extremely small particle diameter catalyst having a particle diameter of 30 µm or less. On the contrary, the catalyst having a small metal deposition amount has a short holding time in the apparatus. For this reason, the ratio of the particle diameter of 30 micrometers or less in the catalyst used for regeneration can be reduced. As a result, it is possible to reduce the loss of the catalyst in the apparatus or the incorporation of the catalyst into the C heavy oil, which is caused by incorporation into fly ash or undigested oil outside the apparatus.

Claims (2)

In a fluid catalytic cracking process including a magnetic separator, magnetic separation of the fluid catalytic cracking catalyst is introduced into a magnetic separator after adjusting the amount of water of the catalyst extracted from the fluid catalytic cracking apparatus to 5 mass% or less. Way. The magnetic separation method according to claim 1, wherein the temperature of the extracted catalyst is adjusted to 100 ° C or lower, and then introduced into a magnetic separation device.