CN217549990U - Catalyst fluidization abrasion grading device - Google Patents

Abstract

The utility model provides a catalyst fluidization abrasion grading device, which consists of a catalyst storage system, a catalyst fluidization abrasion system and a catalyst grading system; the catalyst storage system consists of a catalyst storage tank and a gas carrying pipe; the catalyst fluidization abrasion system consists of a fluidization abrasion reactor, a catalyst feeding pipe and an auxiliary fluidization pipeline, wherein a catalyst primary collision abrasion area is arranged on the catalyst feeding pipe, and a catalyst secondary collision abrasion area is formed at the outlet of the catalyst feeding pipe and the bottom of the fluidization abrasion reactor; the catalyst grading system consists of a first-stage cyclone separator and a second-stage cyclone separator. The device aims at carrying out fluidization abrasion and classification on the catalyst so as to reduce the abrasion of the catalyst in a reaction device, reduce the generation of fine powder, reduce the solid content of slurry oil of the device, reduce the problems of smoke machine faults and the like caused by the fine powder, and ensure the long-period stable operation of the device through the optimization of particle size distribution.

Description

Catalyst fluidization abrasion grading device

Technical Field

The utility model relates to a catalyst technical field, concretely relates to catalyst fluidization abrasion grading plant.

Background

Catalytic cracking is an important means for heavy oil conversion, and maintaining good activity and selectivity of a catalyst is a key for guaranteeing normal operation of a device and improving benefits. The catalyst is deactivated and reactivated by circulating between the reactor and the regenerator, but the catalyst particle size is easily reduced due to the abrasion of the raw oil, the nozzle and the like in the reactor to the catalyst, the abrasion between the catalyst particles in the regenerator and the abrasion between the particles and equipment, and the generated catalyst fine powder enters flue gas and oil gas. The rising of the catalyst fine powder content in flue gas and oil gas easily causes the loss of the catalyst, and the loss of a large amount of the catalyst can cause the reduction of the catalyst inventory and the abnormal fluidization, thereby influencing the normal production of the device. The leaked and damaged catalyst fine powder enters a flue gas and oil slurry pipeline system to accelerate the abrasion of equipment and pipelines, so that the safety production of the device is influenced; at the same time, the catalyst consumption is too high and the cost is increased. The particle size distribution of the fresh catalyst, in particular the content of fines with a particle size of less than 40 μm, and the mechanical strength of the catalyst therefore often determine the operating conditions of the plant and the consumption of catalyst.

Generally, a catalytic cracking catalyst is industrially produced by a spray drying forming process, and in the preparation process, the appearance, the particle size distribution and the mechanical strength of a fresh catalyst are influenced by various factors such as the properties of raw materials, the formula of the catalyst, spraying conditions (temperature, nozzle pressure and the like), roasting, hydrothermal treatment and the like. Therefore, the problems of recess, crack, adhesion and the like often occur in the catalyst product particles produced in industry, and the catalyst particles with the problems are easy to be thermally disintegrated under hydrothermal conditions and easy to be worn and broken in the fluidization process to generate a large amount of fine powder; on the other hand, in the spray forming process, the particle diameter of the catalyst is normally distributed, the catalyst particles with the particle diameter of less than 40 micrometers usually account for 10 to 30 percent of the total weight of the catalyst, and when the preparation of the catalyst or the operation of a spraying device is unstable, the proportion of fine powder is further increased. After fine powder in the catalyst enters a system, the load of the triple rotation is increased; if the separation effect is poor, the catalyst content at the inlet of the smoke machine is high, and the long-period operation of the smoke machine is influenced. In the aspect of a settler, when the content of fine powder in a catalyst is high, the fine powder is easily brought into a fractionating tower by oil gas, so that the catalyst in oil slurry is increased or the solid content of the oil slurry is increased, the operation period of an oil slurry pump is shortened, and great hidden danger is brought to the safe operation of a device.

In order to solve the above problems, the conventional method is to reduce the content of fine powder in the catalyst by means of catalyst production process adjustment, formula optimization, fine powder circulation and other measures. For example, CN201510472307.6 discloses a preparation method of FCC catalyst for reducing the product of ex-situ crystallization reaction, which can effectively reduce the generation of fine powder in the synthesis of FCC catalyst by controlling the crystallization reaction under different temperature gradients. However, this method is accompanied by problems of small pore volume and low content of active components of the catalyst while increasing the mechanical strength of the catalyst, and causes a loss of the reaction performance of the catalyst.

There are also methods for reducing catalyst fines in a catalytic cracker system by taking measures. Patent CN201610384174.1 discloses a device and a method for recovering catalytic cracking catalyst fines, wherein fines are collected by a fines collector after passing through a continuous regeneration device and before entering a reactor, and after pollution metals are effectively treated, the fines are ground by a double colloid method and pulped to regenerate a catalytic cracking (FCC) catalyst in accordance with normal particle size distribution. Patent CN200480020352.8 discloses a method of contacting a quenched effluent gas stream from an oxygenate to olefin process with a liquid to capture catalyst fines for removal of fines during the reaction process. CN103611581A discloses a method for recovering catalyst fine powder for re-granulation, which is suitable for alcohol ether to olefin fluidized bed system, wherein the catalyst fine powder is collected by a dust remover, and the collected catalyst fine powder is directly fed into the catalyst granulation process. The above-mentioned processes often require the addition of a separate device for collecting fines inside the catalytic cracking unit, which increases the complexity and cost of the unit and also affects the circulation fluidization of the catalyst inside the unit.

In addition, in order to reduce fine powder in the catalyst, CN104858044B discloses a method of classifying a catalyst carrier, which performs cyclone classification on a dispersion liquid containing a catalyst carrier, and obtains a dispersion liquid containing a target catalyst carrier in a target particle diameter range by controlling conditions of the cyclone classification. CN206009234U discloses a reforming catalyst negative pressure fluidization windmill type physical grading device. The method has a certain particle grading effect, but is not suitable for a catalytic cracking catalyst with a small particle size, and cannot realize the pre-abrasion effect of the catalyst.

In summary, aiming at the problems of high fine powder content of the catalytic cracking catalyst, poor appearance and the like in industrial application, which easily cause the catalyst to generate fine powder, the existing solutions and technologies have the following problems: 1) There are no devices and methods for specifically addressing catalyst attrition; 2) In order to improve the abrasion resistance, the catalytic performance of the catalyst is sacrificed, but the problem of more fine catalyst powder cannot be avoided; 3) The existing grading device is not suitable for grading treatment of the catalytic cracking catalyst, and the grading effect is not ideal.

SUMMERY OF THE UTILITY MODEL

To the problem, the utility model provides a catalyst fluidization abrasion grading plant through carrying out fluidization abrasion preliminary treatment to industrial catalyst, wears out the granule that easily produces the farine in the catalyst in advance and handles, grades through multistage whirlwind again, controls the within range that is suitable for the device long period running with catalyst particle diameter to the fine powder content in the realization reduction catalyst guarantees the purpose of device even running.

The utility model adopts the following technical scheme:

a catalyst fluidization abrasion grading device comprises a catalyst storage system, a catalyst fluidization abrasion system and a catalyst grading system which are sequentially communicated; the catalyst storage system comprises a catalyst storage tank and a gas carrying pipeline, wherein a discharge valve is arranged at the bottom of the catalyst storage tank and is connected with the gas carrying pipeline through the discharge valve; the gas-carrying pipeline is also connected with a rapid gas-carrying pipeline, and the rapid gas-carrying pipeline is provided with a gas outlet valve; the catalyst fluidized abrasion system comprises a fluidized abrasion reactor, a catalyst feeding pipe is inserted into the side wall of the fluidized abrasion reactor, one end of the catalyst feeding pipe is communicated with a gas carrying pipe, the other end of the catalyst feeding pipe vertically extends to the bottom of the fluidized abrasion reactor downwards, and a gap is formed between the catalyst feeding pipe and the bottom of the fluidized abrasion reactor; a first auxiliary fluidization pipeline and a second auxiliary fluidization pipeline are also inserted in the side wall of the fluidized wear reactor and are symmetrically distributed along the central axis of the fluidized wear reactor; the catalyst classification system comprises a plurality of cyclone separators which are connected in series in sequence, and the first cyclone separator is connected with the fluidized abrasion reactor.

The utility model discloses following beneficial effect has:

by carrying out abrasion pretreatment on an industrial sample of the catalytic cracking catalyst, the catalyst particles which have poor mechanical strength and are easy to abrade to generate fine powder (such as adhesion of a plurality of microspheres, irregular shape, poor sphericity, existence of defects of pits, cracks and the like on the particle surface) and the catalyst particles with large particle size in the catalyst are subjected to abrasion pretreatment, so that the effect of improving the catalyst strength is achieved. After the abrasion pretreatment is finished, the pressure and the gas velocity of the separator are strictly controlled through the multi-stage cyclone separator, the abraded catalyst is classified according to the particle size, fine powder in the catalyst is removed, the fluency of fluidization, circulation and regeneration processes of the catalytic cracking device is improved, the running stability of the catalytic cracking device is improved, and the method has important guiding significance for long-period cyclic utilization of the catalytic cracking catalyst. Meanwhile, the fluidized abrasion grading device has the characteristics of simple operation, good grading effect and strong operation continuity.

Drawings

FIG. 1 is a schematic view of a catalyst fluidization abrasion classification apparatus according to the present invention;

in the figure, 1-a catalyst storage tank, 2-a discharge valve, 3-a gas carrying pipeline, 4-a gas outlet valve, 5-a rapid gas carrying pipeline, 6-a fluidized abrasion reactor, 7-a first auxiliary fluidized pipeline, 8-a secondary collision abrasion area, 9-a second auxiliary fluidized pipeline, 10-a catalyst feeding pipe, 11-a primary collision abrasion area, 12-a catalyst conveying pipe, 13-a primary cyclone separator, 14-a secondary cyclone separator and 15-an emptying pipeline.

Detailed Description

The invention will be further explained with reference to the drawings and the specific embodiments.

As shown in fig. 1, a catalyst fluidization abrasion classification device comprises a catalyst storage system, a catalyst fluidization abrasion system and a catalyst classification system which are sequentially communicated;

the catalyst storage system comprises a catalyst storage tank 1 and a gas carrying pipe line 3, wherein the bottom of the catalyst storage tank 1 is provided with a discharge valve 2 and is connected with the gas carrying pipe line 3 through the discharge valve 2; the gas-carrying pipeline 3 is also connected with a rapid gas-carrying pipeline 5, and the rapid gas-carrying pipeline 5 is provided with a gas outlet valve 4; when in use, the ratio of the apparent gas velocity of the gas carrying pipeline 3 to the apparent gas velocity of the rapid gas carrying pipeline 5 is 1.5-5.

The catalyst fluidization abrasion system comprises a fluidization abrasion reactor 6, a catalyst feeding pipe 10 is inserted into the side wall of the fluidization abrasion reactor 6, one end of the catalyst feeding pipe 10 is communicated with the gas carrying pipeline 3, the other end of the catalyst feeding pipe extends downwards and vertically to the bottom of the fluidization abrasion reactor 6, and a gap is formed between the catalyst feeding pipe 10 and the bottom of the fluidization abrasion reactor 6; a first auxiliary fluidizing line 7 and a second auxiliary fluidizing line 9 are also plugged into the side wall of the fluidized wear reactor 6, and the first auxiliary fluidizing line 7 and the second auxiliary fluidizing line 9 are symmetrically distributed along the central axis of the fluidized wear reactor 6.

When in use, no special requirements are required on the configuration of the fluidized abrasion reactor 6, and the conventional columnar, conical or truncated cone-shaped reactor can realize the fluidized abrasion effect of the catalyst. Preferably, the fluidized abrasion reactor 6 has a conical upper part, a columnar middle part and an inverted conical bottom part, and the ratio of the diameter to the vertical height of the fluidized abrasion reactor 6 is 1:2 to 5; the bottom of an inverted cone-shaped section of the fluidized wear reactor 6 is a secondary collision wear area 8, the vertical section of the secondary collision wear area 8 is in an elliptical arc shape, the long axis of the elliptical arc is vertical to the outlet direction of a catalyst feeding pipe 10, and the ratio of the long axis to the short axis is 1 to 3:1. preferably, the instantaneous linear velocity of the catalyst particles and the gas stream through the secondary impingement wear zone 8 is not less than 3m/s, and more preferably not less than 5m/s.

The bottom of the fluidized abrasion reactor 6 is designed into an inverted cone shape so as to quickly reduce the linear velocity of catalyst particles after the direction of the catalyst particles is changed, thereby forming a dense bed layer of the catalyst at the bottom of the reactor, strengthening the abrasion among the particles, grinding off small particles adhered in the catalyst and achieving the purpose of improving the sphericity of the catalyst; the middle part is designed into a column shape, which is beneficial to forming a uniform dense-phase fluidized bed layer in the reactor, and the height of a dilute phase zone generated by particle entrainment at the interface of the dense-phase bed layer is reduced, so that the abrasion uniformity of the catalyst is improved, and the treatment efficiency is improved; the top is designed into a cone shape, so that when the catalyst is conveyed out of the reactor along with the fluidized gas, the catalyst bed layer is favorably and quickly converted from a turbulent bed into a conveying bed, the purpose of quickly conveying the catalyst is achieved, meanwhile, dead zones in the catalyst bed layer are reduced, and the fluidization quality and the treatment efficiency are improved.

Catalyst feed 10 can enter the fluidized attrition reactor 6 from any location within the fluidized attrition reactor 6, such as a sidewall, a bottom, etc., so long as delivery of catalyst into the fluidized attrition reactor 6 is achieved. Preferably, the catalyst feeding pipe 10 is L-shaped, one end of the catalyst feeding pipe is inserted into the upper side wall of the fluidized abrasion reactor 6, and the other end of the catalyst feeding pipe vertically extends to the position above the secondary collision abrasion area 8 along the central axis of the fluidized abrasion reactor 6; the bending section of the catalyst feeding pipe 10 is a primary collision abrasion zone 11, and preferably, the instantaneous linear speed of catalyst particles and airflow passing through the primary collision abrasion zone 11 is not less than 5m/s, and further preferably, the instantaneous linear speed is not less than 10m/s.

The function of the first-stage collision wear area 11 is as follows: on one hand, catalyst particles entering the fluidized abrasion reactor 6 at a high speed collide with the inner wall of the primary collision abrasion zone 11 strongly to achieve the effect of collision abrasion; on the other hand, the catalyst and the gas flow are changed in direction, and the catalyst is conveyed into the fluidized attrition reactor 6. In order to increase the collision efficiency and reduce the interference of the reflection of the catalyst particles after collision to the forward high-speed catalyst flow, the first-stage collision abrasion area 11 is curved in an arc shape, the vertical section of the first-stage collision abrasion area 11 is an involute, the r of the involute is 1-2 times of the radius of the catalyst feeding pipe 10, and the spread angle of the involute is preferably 70-90 degrees. The secondary impingement wear zone 8 functions similarly to the primary impingement wear zone 11, and functions as impingement wear while changing the direction of catalyst flow.

Meanwhile, in order to uniformly carry out fluidization abrasion and transportation on catalyst particles in the fluidization abrasion reactor 6, a plurality of first auxiliary fluidization pipelines 7 and second auxiliary fluidization pipelines 9 are arranged on the side wall of the fluidization abrasion reactor 6, and the first auxiliary fluidization pipelines 7 and the second auxiliary fluidization pipelines 9 can be arranged on the side wall of the middle columnar section of the fluidization abrasion reactor 6 or on the side wall of the bottom inverted-conical section, so that the purposes can be achieved. Preferably, the total number of the first auxiliary fluidization pipeline 7 and the second auxiliary fluidization pipeline 9 is 2 to 12, the first auxiliary fluidization pipeline 7 and the second auxiliary fluidization pipeline 9 are symmetrically distributed on the side wall of the bottom inverted cone-shaped section along the central axis of the fluidized abrasion reactor 6, and the included angles between the first auxiliary fluidization pipeline 7 and the bottom inverted cone-shaped side wall of the fluidized abrasion reactor 6 and the first auxiliary fluidization pipeline 9 are 60 to 90 degrees; the intersection points of the first auxiliary fluidization line 7 and the second auxiliary fluidization line 9 with the bottom inverted cone-shaped side wall of the fluidized attrition reactor 6 are located at 1/3-2/3 of the vertical height of the bottom inverted cone-shaped section.

The catalyst classification system consists of a plurality of cyclone separators connected in series. Preferably, the catalyst classification system consists of a primary cyclone 13 and a secondary cyclone 14 in series. The primary cyclone 13 is connected to the fluidized attrition reactor 6 via a catalyst transfer line 12 and is connected in series with the secondary cyclone 14. The outlet of the secondary cyclone 14 is connected to an evacuation line 15. The utility model discloses there is not special requirement to the structure of one-level cyclone 13 and second grade cyclone 14, and hierarchical purpose can be realized to the cyclone homoenergetic of field conventionality.

In order to achieve the purposes of optimizing the fluidization state of a catalytic cracking unit, reducing fine catalyst powder and reducing the solid content of oil slurry through a catalyst classification system, the particle size range of the catalyst obtained by the first-stage cyclone separator 13 is preferably 30 to 150 micrometers, the particle size range of the catalyst obtained by the second-stage cyclone separator 14 is not more than 45 micrometers, and the particle size of fine powder discharged by the emptying pipeline 15 is not more than 10 micrometers. Further preferably, the particle size of the catalyst obtained by the primary cyclone separator 13 is 40 to 130 micrometers, and the particle size of the catalyst obtained by the secondary cyclone separator 14 is 8 to 40 micrometers; the fine powder discharged from the emptying line 15 has a particle size of not more than 8 μm.

The utility model discloses there is not special requirement to the fluidization gas kind and the temperature in carrier gas pipeline 3 and the quick carrier gas pipeline 5, and conventional fluidization gas homoenergetic plays fluidization, wearing and tearing, hierarchical effect, like air, nitrogen gas, vapor, helium etc. can be one of conventional fluidization gas, also can be the mixture of concentrated gas. In order to further enhance the abrasion of the catalyst and reduce the fluidization abrasion time, one or more of high-temperature nitrogen, air and superheated steam are preferably used as a fluidizing medium, the temperature of the fluidizing medium is 50-1000 ℃, and the temperature of the fluidizing gas is further preferably 100-800 ℃. If the field condition can not make the gas reach the required temperature condition, a heating device can be arranged on the outer wall of the fluidized abrasion reactor 6 to ensure that the constant temperature of the catalyst bed layer is in the temperature range.

The working process of the utility model is as follows:

filling a certain amount of industrial samples of the catalytic cracking catalyst into a catalyst storage tank 1 of a catalyst storage system, opening a catalyst discharge switch valve 2 below the catalyst storage tank 1, enabling the catalyst to slide into a gas carrying pipeline 3, and enabling the catalyst to flow along the gas carrying pipeline 3 under the carrying of fluidizing gas; the on-off valve 4 on the fast gas carrying pipeline 5 is opened, and the high-temperature and fast fluidizing gas from the fast gas carrying pipeline 5 is converged with the catalyst gas flow in the gas carrying pipeline 3 to form high-speed flowing catalyst gas flow which enters the catalyst feeding pipe 10. The high velocity catalyst gas stream flows along the catalyst feed pipe 10 and undergoes intense collisions within the primary collision wear zone 11 to break the breakable catalyst particles in the catalyst industry sample into small particles and change the direction of flow. The high-speed catalyst gas flow with changed flow direction is vertically conveyed to the bottom of the fluidized abrasion reactor 6 along the catalyst feeding pipe 10, and further collides in the secondary collision abrasion zone 8, and the catalyst sample subjected to two-stage abrasion gradually accumulates at the lower part of the fluidized abrasion reactor 6 to form a catalyst bed layer. When the catalyst in the catalyst storage tank 1 is completely conveyed into the fluidized attrition reactor 6, the catalyst discharge switch valve 2 and the switch valve 4 on the rapid gas carrying line 5 are closed, and the fluidizing gas in the gas carrying line 3 keeps constant flow velocity and flow rate and enters the fluidized attrition reactor 6 along the catalyst feeding pipe 10 to play a role of fluidizing the catalyst.

High-temperature fluidizing gas enters the fluidized attrition reactor 6 from a first auxiliary fluidizing line 7 and a second auxiliary fluidizing line 9 in the lower part of the fluidized attrition reactor 6, and fluidizes and attrites the catalyst particles in the fluidized attrition reactor 6. Under the combined action of the multiple fluidizing gases injected from the catalyst feeding pipe 10, the first auxiliary fluidizing line 7 and the second auxiliary fluidizing line 9, the catalyst particles are uniformly and sufficiently contacted with the fluidizing gas, and uniform abrasion of the catalyst particles is ensured.

After the catalyst is fluidized and abraded, opening a switch valve 4 on a rapid gas carrying pipeline 5, increasing the gas velocity of fluidizing gas in auxiliary fluidizing pipelines 7 and 9, and rapidly conveying catalyst particles in a fluidized and abraded reactor 6 into a catalyst grading system; the catalyst particles subjected to fluidization abrasion are firstly conveyed into a primary cyclone separator 13, the catalyst particles with the particle size range of 30-150 micrometers are obtained at the bottom of the primary cyclone separator 13, the gas carrying fine particles leave from the top of the primary cyclone separator 13 and enter a secondary cyclone separator 14, the catalyst particles with the particle size of 20-40 micrometers are obtained at the bottom of the secondary cyclone separator, and the catalyst particles with the particle size of less than 10 micrometers leave the system from an evacuation pipeline 15 at the top of the secondary cyclone separator 14. And finally, mixing the bottom products obtained by the primary cyclone separator 13 and the secondary cyclone separator 14 according to the requirements of different industrial devices on the particle size distribution of the catalyst.

The effect of the use of the catalyst fluidization attrition device is further illustrated with reference to the examples below.

Comparative example

The commercially available industrial catalytic cracking catalyst products were used as comparative examples, and the particle size distribution and attrition index thereof were measured without carrying out attrition pretreatment, and the results are shown in Table 1.

Example 1

A catalyst fluidization attrition classification apparatus, which was composed of a catalyst storage system, a catalyst fluidization attrition system, and a catalyst classification system, was fabricated as shown in fig. 1. The catalyst storage system consists of a catalyst storage tank, a gas carrying pipeline and a quick gas carrying pipeline, and the ratio of the apparent gas velocity of the gas carrying pipeline 3 to the apparent gas velocity of the quick gas carrying pipeline 5 is 1. The catalyst fluidization attrition system consists of a fluidization attrition reactor 6, a catalyst feed pipe 10, a first auxiliary fluidization line 7 and a second auxiliary fluidization line 9. A catalyst feed 10 is connected to the gas carrier line 3 of the catalyst storage system and the catalyst feed 10 enters from the upper side wall of the fluidized attrition reactor and extends vertically along the central axis to the bottom of the fluidized attrition reactor 6. An arc-shaped primary collision abrasion area 11 is arranged at the corner of a catalyst feeding pipe 10, the vertical section of the primary collision abrasion area 11 is an involute, the radius of the involute is 1.5 times of the radius of the catalyst feeding pipe, and the included angle of the involute is preferably 80 degrees. The instantaneous linear velocity of the catalyst particles and the gas stream through the primary zone 11 of impingement wear is 10m/s. The lower part of the fluidized abrasion reactor 6 is in an inverted cone shape, the middle part is in a column shape, and the upper part is in a cone shape; the ratio of its diameter to vertical height is 1. The bottom of the fluidized abrasion reactor 6 and the position corresponding to the outlet of the catalyst feeding pipe 10 are provided with a secondary collision abrasion area 8, the secondary collision abrasion area 8 is of a concave spherical shape, the vertical section of the secondary collision abrasion area is of an elliptic arc shape, and the ratio of the long axis of the elliptic arc to the short axis of the elliptic arc is 3. The instantaneous linear velocity of the catalyst particles and the gas stream through the secondary zone 8 of impingement wear is 8m/s. The bottom inverted cone side wall of the fluidized abrasion reactor 6 is provided with 2 first auxiliary fluidization pipelines 7 and second auxiliary fluidization pipelines 9 which are symmetrically distributed along the central axis, the included angle between each auxiliary fluidization pipeline and the bottom inverted cone side wall of the fluidized abrasion reactor 6 is 70 degrees, and the intersection point of each auxiliary fluidization pipeline and the bottom inverted cone side wall is positioned at 1/2 of the vertical height of the bottom inverted cone.

The catalyst classification system is composed of a first-stage cyclone separator 13 and a second-stage cyclone separator 14 which are connected in series. The first-stage cyclone separator can obtain catalyst particles of 40 to 130 micrometers, and the second-stage cyclone separator can obtain catalyst particles of 8 to 40 micrometers; the fine powder in the evacuation line 15 has a particle size of not more than 8 microns. The fluidizing gas was high temperature nitrogen at 700 ℃.

The same commercial industrial catalytic cracking catalyst product of comparative example 1 was used as a pretreatment on the fluid attrition classifier as described in example 1, and the particle size distribution and attrition index were measured and reported in table 1.

Example 2

A fluidized attrition classifier for a catalyst was prepared as shown in FIG. 1, except that in example 2, no fast carrier gas line 5 was used, and only the corners of the catalyst feed pipe were provided with primary zone 11 and no secondary zone 8. And the vertical section of the first-stage collision abrasion zone 11 is an involute, the radius of the involute is 2 times of the radius of the catalyst feeding pipe, and the included angle of the involute is preferably 90 degrees. The instantaneous linear velocity of the catalyst particles and the gas stream through the primary zone of impingement attrition was 5m/s. The fluidizing gas was high temperature steam at 500 ℃. The rest is the same as in example 1.

The same commercial industrial catalytic cracking catalyst product of comparative example 1 was used as a pretreatment on the fluid attrition classifier of example 2, and the particle size distribution and attrition index were measured and reported in table 1.

Example 3

A catalyst fluidized attrition classifier was fabricated as shown in fig. 1, except that in example 3, no primary impingement wear zone was provided at the corners of the feed line, and only a secondary impingement wear zone 8 was provided, unlike in example 1. The vertical cross section of the secondary collision abrasion area is in an elliptic arc shape, and the ratio of the long axis to the short axis of the elliptic arc shape is 2. The instantaneous linear velocity of the catalyst particles and the gas stream through the secondary impingement wear zone was 10m/s. The rest is the same as in example 1.

The same commercial industrial catalytic cracking catalyst product of comparative example 1 was used as a pretreatment on the fluid attrition classifier of example 2, and the particle size distribution and attrition index were measured and reported in table 1.

TABLE 1 catalyst particle size distribution and attrition index

As can be seen from Table 1 above, compared with the comparative example, the fine powder content of 0 to 40 μm in the catalyst is obviously reduced in example 1, and meanwhile, the large particles of more than 149 μm are obviously reduced, the attrition index of the catalyst is obviously improved, which is mainly that the catalyst fluidization attrition classification device can abrade irregular catalyst particles in the catalyst and remove the irregular catalyst particles in the form of fine powder.

Claims (8)

1. A catalyst fluidization attrition classification apparatus characterized by: the device comprises a catalyst storage system, a catalyst fluidization abrasion system and a catalyst grading system which are sequentially communicated;

the catalyst storage system comprises a catalyst storage tank (1) and a gas carrying pipe line (3), wherein a discharge valve (2) is arranged at the bottom of the catalyst storage tank (1) and is connected with the gas carrying pipe line (3) through the discharge valve (2); the air-carrying pipeline (3) is also connected with a rapid air-carrying pipeline (5), and the rapid air-carrying pipeline (5) is provided with an air outlet valve (4);

the catalyst fluidization abrasion system comprises a fluidization abrasion reactor (6), a catalyst feeding pipe (10) is inserted into the side wall of the fluidization abrasion reactor (6), one end of the catalyst feeding pipe (10) is communicated with the gas carrying pipe line (3), the other end of the catalyst feeding pipe (10) vertically extends to the bottom of the fluidization abrasion reactor (6) downwards, and a gap is formed between the catalyst feeding pipe and the bottom of the fluidization abrasion reactor (6); a first auxiliary fluidization pipeline (7) and a second auxiliary fluidization pipeline (9) are also inserted in the side wall of the fluidized abrasion reactor (6), and the first auxiliary fluidization pipeline (7) and the second auxiliary fluidization pipeline (9) are symmetrically distributed along the central axis of the fluidized abrasion reactor (6);

the catalyst classification system comprises a plurality of cyclone separators which are connected in series in sequence, and the first cyclone separator is connected with the fluidized abrasion reactor (6).

2. A catalyst fluidization abrasion classification apparatus according to claim 1, characterized in that: the upper part of the fluidized abrasion reactor (6) is conical, the middle part is columnar, and the bottom part is inverted conical; and the ratio of the diameter to the vertical height of the fluidized attrition reactor (6) is 1:2 to 5.

3. A catalyst fluidization attrition classification apparatus in accordance with claim 2 wherein: the bottom of the inverted cone-shaped section of the fluidized wear reactor (6) is a secondary collision wear area (8), the vertical section of the secondary collision wear area (8) is in an elliptical arc shape, and the ratio of the long axis to the short axis of the elliptical arc is 1 to 3:1.

4. a catalyst fluidization attrition classification apparatus in accordance with claim 2 wherein: the first auxiliary fluidization pipeline (7) and the second auxiliary fluidization pipeline (9) are positioned at 1/3-2/3 of the vertical height of the inverted cone section at the bottom of the fluidized abrasion reactor (6), and the included angle between the first auxiliary fluidization pipeline (7) and the second auxiliary fluidization pipeline (9) and the side wall of the inverted cone section at the bottom of the fluidized abrasion reactor (6) is 60-90 degrees.

5. A catalyst fluidization attrition classification apparatus as claimed in claim 2 wherein: the total number of the first auxiliary fluidization lines (7) and the second auxiliary fluidization lines (9) is 2 to 12.

6. A catalyst fluidization abrasion classification apparatus according to claim 1, characterized in that: the catalyst feeding pipe (10) is L-shaped, and the bending section of the catalyst feeding pipe (10) is a first-stage collision wear area (11).

7. The catalyst fluidization abrasion classification apparatus according to claim 6, wherein: the primary collision abrasion area (11) is curved in an arc shape, the vertical section of the primary collision abrasion area (11) is in an involute shape, the base radius of the involute is 1 to 2 times of the radius of the catalyst feeding pipe (10), and the spread angle of the involute is 70 to 90 degrees.

8. A catalyst fluidization abrasion classification apparatus according to claim 1, characterized in that: the catalyst grading system comprises a primary cyclone separator (13) and a secondary cyclone separator (14), wherein the inlet end of the primary cyclone separator (13) is connected with a catalyst conveying pipe (12) and is connected with the top of the fluidized abrasion reactor (6) through the catalyst conveying pipe (12); the inlet end of the secondary cyclone separator (14) is connected with the outlet end of the primary cyclone separator (13), and the outlet end of the secondary cyclone separator (14) is connected with an emptying pipeline (15).

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