CN111282815A - Solid particle size controller, application thereof and method for separating solid particles - Google Patents
Solid particle size controller, application thereof and method for separating solid particles Download PDFInfo
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- CN111282815A CN111282815A CN201811495644.7A CN201811495644A CN111282815A CN 111282815 A CN111282815 A CN 111282815A CN 201811495644 A CN201811495644 A CN 201811495644A CN 111282815 A CN111282815 A CN 111282815A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B07—SEPARATING SOLIDS FROM SOLIDS; SORTING
- B07B—SEPARATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, SIFTING OR BY USING GAS CURRENTS; SEPARATING BY OTHER DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
- B07B7/00—Selective separation of solid materials carried by, or dispersed in, gas currents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B07—SEPARATING SOLIDS FROM SOLIDS; SORTING
- B07B—SEPARATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, SIFTING OR BY USING GAS CURRENTS; SEPARATING BY OTHER DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
- B07B11/00—Arrangement of accessories in apparatus for separating solids from solids using gas currents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B07—SEPARATING SOLIDS FROM SOLIDS; SORTING
- B07B—SEPARATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, SIFTING OR BY USING GAS CURRENTS; SEPARATING BY OTHER DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
- B07B11/00—Arrangement of accessories in apparatus for separating solids from solids using gas currents
- B07B11/04—Control arrangements
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B07—SEPARATING SOLIDS FROM SOLIDS; SORTING
- B07B—SEPARATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, SIFTING OR BY USING GAS CURRENTS; SEPARATING BY OTHER DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
- B07B11/00—Arrangement of accessories in apparatus for separating solids from solids using gas currents
- B07B11/06—Feeding or discharging arrangements
Abstract
The invention relates to the technical field of petroleum processing, and discloses a solid particle size controller and a method for separating solid particles, wherein the size controller comprises: the first separation zone (A) is used for separating the large-particle regenerant and the medium-particle size regenerant, the first separation zone contains a separation unit (11) and a transmission unit (9) connected with the separation unit (11), the upper part of the separation unit is provided with a feed inlet (1), the lower part of the separation unit is provided with a first gas inlet (2), and the bottom of the separation unit is provided with a first discharge hole (8) for leading out the large-particle regenerant; and the second separation zone (B) is used for separating the medium-particle size regenerant and the small-particle size regenerant, and the lower part of the second separation zone (B) is provided with a third gas inlet (4) and a second discharge hole (7) for leading out the medium-particle size regenerant. The solid particle size controller of the invention can realize classification of different particles.
Description
Technical Field
The invention relates to the technical field of petroleum processing, in particular to a solid particle size controller, application thereof and a method for separating solid particles.
Background
With the development of the world economy, the demand of light and clean fuel oil for human beings is rapidly increased. However, the crude oil has a high degree of heaviness and deterioration worldwide (mainly manifested by high density, high viscosity, high carbon residue, high heavy metal content, high sulfur and nitrogen content, etc.), and environmental standards of countries worldwide are becoming strict, and these factors present many new problems for the oil refining industry.
Currently, the heavy oil processing is mainly divided into two types, decarburization and hydrogenation, from the mechanical point of view.
Hydrogenation mainly comprises hydrofining and hydrocracking. The hydrogenation process has important significance for improving the processing depth of crude oil, improving the quality of products and improving the yield of light oil products; however, the heavy oil hydrogenation process has high operation temperature and pressure, but has low conversion rate, usually about 30 to 50 wt%. Meanwhile, hydrogenation of crude oil requires a large amount of hydrogen, and the source of the hydrogen is a difficult problem which always troubles the oil refining industry.
The decarbonization process is the main method for processing the heavy oil at present, and mainly comprises heavy oil catalytic cracking, solvent deasphalting and delayed coking. The heavy oil catalytic cracking is a catalytic process, so that not all raw materials can be directly subjected to catalytic cracking without pretreatment, the carbon residue of raw oil for domestic heavy oil catalytic cracking is generally controlled to be 4-6 wt%, and the metal content is controlled to be not more than 10 mug/g. Delayed coking is a heavy oil processing method with the highest conversion depth, and more than 60 percent of the oil residues abroad are adopted by the method at present, and the method has the defect of low liquid product yield; and when the delayed coking process is adopted to process the sulfur-containing residual oil, the sulfur content of the coke is high, and the problem exists in the process of going out.
The cracking-gasification integrated process of heavy and poor raw oil gives consideration to oil refining and gas making for hydrogen production, and has obvious advancement in the aspects of processing poor heavy oil and improving the efficient utilization of low-quality carbon. The inferior oil fluid coking process and the flexible coking process developed by Mobil corporation in the United states are the beginning of the cracking-gasification integrated process. Both of them use coke nucleus as fluidizing medium and coke and heat carrier, but the method has the problems of uneven particle size distribution of coke particles, easy generation of larger lumps and fine coke powder, etc., and influences the fluidizing effect.
ART process of Engerhal company, FTC process of Japan Fuji oil company, 3D and MSCC process of America and ROP process of China all carry out shallow treatment to residual oil by decarburization while reaction, deposited coke carried by adopted heat carrier or catalyst is supplied by combustion heat release and regeneration is completed at the same time, but all have the problems of low energy utilization rate, low residual oil conversion rate and the like.
Therefore, the development of a new method for converting heavy and poor raw oil has very important practical significance.
CN1400159A discloses a method for producing hydrogen by using catalytic cracking regenerated flue gas, in which a catalyst deposited with carbon after catalytic cracking reaction is sent to a first regenerator, and after the catalyst is contacted with an oxygen-containing gas at the temperature of 500-660 ℃, CO in the obtained regenerated flue gas is subjected to a shift reaction with water vapor to obtain a hydrogen-rich gas. The semi-regenerant obtained from the first regenerator enters a second regenerator, contacts with oxygen-containing gas, and is regenerated under the conventional catalytic cracking regeneration condition, and the regenerated catalyst returns to the reactor for recycling. The conventional catalytic cracking raw material processed by the method also uses a conventional catalytic cracking catalyst.
CN1504404A discloses a process method combining oil refining and gasification, which utilizes a coke transfer agent to treat residual oil in a riser reactor, on one hand, shallow catalytic cracking or thermal cracking is carried out to generate light components mainly comprising diesel oil or low-carbon hydrocarbons; on the other hand, simultaneous decarburization is carried out, whereby coke is attached to the coke transfer agent together with metals, sulfur, nitrogen and the like. Then, the coke on the coke transfer agent is gasified in the gasification furnace to produce a synthesis gas while regenerating the coke transfer agent. When the method is used for treating poor heavy oil, a large amount of impurities such as metal and the like can be deposited on the contact agent due to high metal content, and due to the increase of the impurities such as metal and the like, the influence on the reaction process is that the activity of the contact agent is reduced, the product selectivity is poor, and the yield of dry gas, hydrogen and coke is increased.
In the contact cracking process of the poor-quality residual oil, the particle size of the coke transfer agent is very important, in order to keep a good fluidized state, the particles must be in a reasonable range, and when the content of coke on the coke transfer agent is high, the particle size is not easily controlled to be between 20 and 80 mu m like catalytic cracking. If too much fine particles are present, sintering occurs, which is detrimental to fluidization. If the large particles are too large, sluggish flow and poor circulation can occur.
Disclosure of Invention
The invention aims to overcome the technical problem that the particle sizes of different particles in a fluidized bed or a riser in the prior art are difficult to control, and provides a novel controller for realizing the particle sizes of solid particles and simultaneously realizing classification of different particles.
In order to achieve the above object, a first aspect of the present invention provides a solid particle size controller comprising:
the first separation area is used for separating the large-particle regenerant and the medium-particle size regenerant, the first separation area contains a separation unit and a transmission unit connected with the separation unit, the upper part of the separation unit is provided with a feed inlet, the lower part of the separation unit is provided with a first gas inlet, and the bottom of the separation unit is provided with a first discharge outlet for leading out the large-particle regenerant;
the second separation area is used for separating medium-particle size regenerant and small-particle size regenerant, one end of the transmission unit in the first separation area is embedded into the second separation area, and the lower part of the second separation area is provided with a third gas inlet and a second discharge hole for leading out the medium-particle size regenerant; a baffle is also disposed in the second separation zone to enable a stream introduced into the second separation zone from the top of the transfer unit to flow toward the bottom of the second separation zone after contacting the baffle; and the top of the second separation zone is provided with a gas-solid separator and a third discharge hole for leading out the small particle regenerant.
The present invention describes that the particle sizes of the large particle regenerant, the medium particle regenerant and the small particle regenerant involved in the structure of the solid particle size controller have no influence on the structure of the solid particle size controller, and the adjectives "large", "medium", "small" and the like are applied only for distinguishing the separation of particles of different sizes at different positions, and those skilled in the art should not be construed as limiting the structure of the present invention.
Preferably, a second gas inlet is also provided in the transfer unit in the first separation zone.
Preferably, a gas distributor is further provided in the first separation zone to enable gas introduced by the first gas inlet to move in the first separation zone towards the transport unit.
Preferably, a gas distributor is further provided in the second separation zone to enable gas introduced by the third gas inlet to move in the second separation zone towards the gas-solid separator.
Preferably, the second gas inlet is arranged in a direction such that gas introduced by the second gas inlet is able to move towards the second separation zone.
Preferably, the first separation area and the second separation area are coaxial with each other.
According to a preferred embodiment, the length of the first separation zone is 10-50% of the total length of the particle size controller, and the length of the first separation zone is the distance between the bottom of the separation unit and the top of the transport unit.
According to a preferred embodiment, the length of the second separation zone is 50-90% of the total length of the particle size controller, and the length of the second separation zone is the distance between the bottom of the second separation zone and the top of the second separation zone.
In the present invention, the total length of the particle size controller is the distance between the bottom of the separation unit and the top of the second separation zone.
Preferably, the separation unit is a hollow reducing cylinder with a thick middle part and two thin ends.
Preferably, the three parts forming the cylinder are respectively a lower part close to the first discharge hole, a truncated cone-shaped middle part and an upper part close to the transmission unit.
The inner diameter of the lower portion may be in the range of 0.1-1m and the height of the lower portion may be in the range of 0.2-2 m.
Preferably, the longitudinal section of the circular truncated cone-shaped middle part is an isosceles trapezoid, and the vertex angle of the isosceles trapezoid is 5-70 degrees.
The inner diameter of the truncated cone-shaped middle part can be in the range of 0.3-30 m.
Preferably, the inner diameter ratio of the circular truncated cone-shaped middle part to the lower part is (1-10): 1.
preferably, the ratio of the inner diameter of the truncated cone-shaped middle part to the inner diameter of the upper part is (1-8): 1.
a second aspect of the invention provides the use of a solid particle size controller as hereinbefore described for separating solid particles.
A third aspect of the present invention provides a method of separating solid particles, the method being performed using the aforementioned particle size controller of the present invention, the method comprising: introducing gas into the particle size controller from a first gas inlet and a third gas inlet, respectively, and introducing solid particles into the separation unit of the first separation zone from the feed inlet, controlling the flow rate of the gas introduced into the particle size controller from the first gas inlet so that large-particle solids in the solid particles are led out from the first discharge port, and causing material containing medium and small particle solids to move upwardly from the transfer unit into the second separation zone, and controlling the separation conditions of the gas-solid separator and controlling the flow rate of gas introduced into the particle size controller from the third gas inlet such that the material containing medium and small particle solids separates the obtained medium and small particle solids in the second separation zone, the medium particle solids are withdrawn from the second discharge, and gas and the small particle solids are withdrawn from the third discharge.
Preferably, the method further comprises: introducing gas into the particle size controller from a second gas inlet.
According to a preferred embodiment, the solid particles are regenerants in the fluidization processing of heavy oils.
Preferably, the flow rate of the gas introduced into the particle size controller from the first gas inlet is controlled to be 0.01 to 0.8m/s, preferably 0.05 to 0.5 m/s.
Preferably, the flow rate of the gas introduced into the particle size controller from the second gas inlet is controlled to be 1 to 38m/s, preferably 2 to 18 m/s.
Preferably, the flow rate of the gas introduced into the particle size controller from the third gas inlet is controlled to be 0.01 to 0.8m/s, preferably 0.05 to 0.5 m/s.
According to a first preferred embodiment, in the method of the present invention, the flow rate of the gas introduced into the particle size controller from the first gas inlet is controlled to be 0.01 to 0.8m/s, the flow rate of the gas introduced into the particle size controller from the second gas inlet is controlled to be 1 to 38m/s, and the flow rate of the gas introduced into the particle size controller from the third gas inlet is controlled to be 0.01 to 0.8 m/s.
According to a second preferred embodiment, in the method of the present invention, the flow rate of the gas introduced into the particle size controller from the first gas inlet is controlled to be 0.05 to 0.5m/s, the flow rate of the gas introduced into the particle size controller from the second gas inlet is controlled to be 2 to 18m/s, and the flow rate of the gas introduced into the particle size controller from the third gas inlet is controlled to be 0.05 to 0.5 m/s.
The inventors of the present invention have found in their research that controlling the method of the present invention within the scope of the first and second preferred embodiments described above enables the size of the medium size solids to be made more uniform when the solid particles are separated by the method of the present invention, thereby enabling better results to be obtained in processes employing medium size solids.
According to a third preferred embodiment, the flow rate of the gas introduced from each gas inlet and the separation conditions of the gas-solid separator are controlled such that the particle size of the large particulate solids withdrawn from the first outlet is greater than 80 μm, wherein particles greater than 100 μm account for 50-95 wt% of the total large particulate solids withdrawn from the first outlet; more preferably, it is 60 to 95 wt% of the total large particulate solids withdrawn from the first outlet.
According to a fourth preferred embodiment, the flow rate of the gas introduced from each gas inlet and the separation conditions of the gas-solid separator are controlled such that the particle size of the small-particle solids withdrawn from the third outlet is less than 20 μm, wherein particles smaller than 10 μm account for 50-95 wt.% of the total small-particle solids withdrawn from the third outlet; more preferably, it is 60 to 95 wt% of the total of the small particle solids withdrawn from the third outlet.
According to a fifth preferred embodiment, the flow rate of the gas introduced from each gas inlet and the separation conditions of the gas-solid separator are controlled such that the average particle size of the medium-sized solids withdrawn from the second outlet is in the range of 20 to 100 μm, preferably 40 to 80 μm.
In the aforementioned preferred embodiment of the present invention, the size division point of the large particle solid and the medium particle solid is preferably 80 to 100 μm, and the size division point of the medium particle solid and the small particle solid is preferably 20 to 40 μm.
Preferably, the conditions in the particle size controller include: the temperature is 350 ℃ and 900 ℃, and the pressure is 0.13-4 MPa.
The solid particles of the present invention may be one or more mixtures of coal, biomass, petroleum coke, inorganic materials, and the like.
Preferably, the solid particles have a density of 0.3 to 3g/cm3。
The gas used for the gas inlet in the particle size controller can be one or more of water vapor, air, oxygen and carbon dioxide.
The particle size controller can work at normal temperature and high temperature, and the working temperature range is 0-1500 ℃, preferably 25-1000 ℃.
Compared with the prior art, when the solid particle size controller is used for separating the regenerant in the process of fluidized processing of heavy oil, the solid particle size controller also has the following beneficial effects:
the invention can control the particle size of solid particles through the particle size controller, realizes good fluidization and ensures the long-period stable operation of the solid particles in the residual oil fluidization processing device.
Drawings
FIG. 1 is a schematic structural diagram of a preferred embodiment of the solid particle size controller of the present invention.
Description of the reference numerals
A. A first separation area B and a second separation area
1. Feed inlet 2, first gas inlet
3. Second gas inlet 4, third gas inlet
5. Gas-solid separator 6, third discharge port
7. Second discharge port 8 and first discharge port
9. Conveying unit 10 and baffle
11. Separation unit
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
The following provides a preferred structure of the solid particle size controller of the present invention and a method for separating solid particles by using the solid particle size controller of the preferred structure of the present invention with reference to fig. 1.
First, as shown in fig. 1, the solid particle size controller of the present invention comprises:
the first separation area A is used for separating the large-particle regenerant and the medium-particle size regenerant, the first separation area A contains a separation unit 11 and a conveying unit 9 connected with the separation unit 11, the upper part of the separation unit is provided with a feed inlet 1, the lower part of the separation unit is provided with a first gas inlet 2, and the bottom of the separation unit is provided with a first discharge outlet 8 for leading out the large-particle regenerant;
a second separation area B for separating medium-particle-size regenerant and small-particle-size regenerant, wherein one end of a transmission unit 9 in the first separation area A is embedded into the second separation area B, and the lower part of the second separation area B is provided with a third gas inlet 4 and a second discharge hole 7 for leading out the medium-particle-size regenerant; a baffle 10 is also provided in the second separation zone B to enable the stream introduced into the second separation zone B from the top of the transfer unit 9 to flow towards the bottom of the second separation zone B after contacting the baffle; the top of the second separation area B is provided with a gas-solid separator 5 and a third discharge hole 6 for leading out the small particle regenerant.
Preferably, a second gas inlet 3 is also provided in the transfer unit 9 in the first separation zone a.
Preferably, a gas distributor is further provided in the first separation zone a to enable the gas introduced by the first gas inlet 2 to move in the first separation zone a towards the transport unit 9.
Preferably, a gas distributor is also provided in the second separation zone B to enable the gas introduced by the third gas inlet 4 to move in the second separation zone B towards the gas-solid separator 5.
Preferably, the second gas inlet 3 is disposed in such a direction that the gas introduced from the second gas inlet 3 can move toward the second separation zone B.
Preferably, the first separation area a and the second separation area B are coaxial with each other.
Preferably, the length of the first separation area a accounts for 10-50% of the total length of the particle size controller.
Preferably, the length of the second separation zone B is 50-90% of the total length of the particle size controller.
Preferably, the separation unit 11 is a hollow variable diameter cylinder with a thick middle and two thin ends.
Then, a preferred method for separating solid particles using the particle size controller of the present invention is provided in connection with fig. 1, the method comprising: introducing gas into the particle size controller from a first gas inlet 2 and a third gas inlet 4, respectively, and introducing solid particles into a separation unit 11 of a first separation zone a from a feed inlet 1, controlling the flow rate of the gas introduced into the particle size controller from the first gas inlet 2 so that large particle solids of the solid particles are withdrawn from a first discharge outlet 8, and moving material containing medium particle solids and small particle solids upward from a transfer unit 9 into a second separation zone B, and controlling the separation conditions of a gas-solid separator 5 and the flow rate of the gas introduced into the particle size controller from the third gas inlet 4 so that the material containing medium particle solids and small particle solids separates the obtained medium particle solids and small particle solids in the second separation zone B, and withdrawing the medium particle solids from a second discharge outlet 7, and withdrawing gas and the small particle solids from a third discharge port 6.
Preferably, the method further comprises: gas is introduced into the particle size controller from a second gas inlet 3.
According to a preferred embodiment, the solid particles are regenerants in the fluidization processing of heavy oils.
Preferably, the flow rate of the gas introduced into the particle size controller from the first gas inlet 2 is controlled to be 0.01 to 0.8m/s, more preferably 0.05 to 0.5 m/s.
Preferably, the flow rate of the gas introduced into the particle size controller from the second gas inlet 3 is controlled to be 1 to 38m/s, more preferably 2 to 18 m/s.
Preferably, the flow rate of the gas introduced into the particle size controller from the third gas inlet 4 is controlled to be 0.01 to 0.8m/s, more preferably 0.05 to 0.5 m/s.
Preferably, the flow rate of the gas introduced from each gas inlet and the separation conditions of the gas-solid separator 5 are controlled so that the particle size of the large particle solids withdrawn from the first outlet port 8 is greater than 80 μm, wherein particles greater than 100 μm account for 50-95 wt% of the total large particle solids withdrawn from the first outlet port 8; more preferably, it is 60 to 95 wt% of the total large particle solids discharged from the first discharge port 8.
Preferably, the flow rate of the gas introduced from each gas inlet and the separation conditions of the gas-solid separator 5 are controlled so that the particle size of the small particulate solids withdrawn from the third outlet 6 is less than 20 μm, wherein particles smaller than 10 μm account for 50-95 wt% of the total small particulate solids withdrawn from the third outlet 6; more preferably, it is 60 to 95 wt% of the total of the small particle solids withdrawn from the third outlet 6.
Preferably, the flow rate of the gas introduced from each gas inlet and the separation conditions of the gas-solid separator 5 are controlled so that the average particle diameter of the medium-sized solids withdrawn from the second discharge port 7 is 20 to 100 μm, preferably 40 to 80 μm.
Preferably, the conditions in the particle size controller include: the temperature is 350 ℃ and 900 ℃, and the pressure is 0.13-4 MPa.
The present invention will be described in detail below by way of examples. The following are laboratory level tests that illustrate the effectiveness of the present and prior art protocols.
The length of the first separation zone a in the solid particle size controller in the following examples accounts for 45% of the total length of the size controller; the length of the second separation zone B accounts for 85% of the total length of the particle size controller.
Example 1
In this example, a solid particle size controller shown in fig. 1 is used to separate the regenerant during the fluidization processing of heavy oil, and the specific parameter conditions are as follows:
the composition of the fresh coke transfer agent used was: al (Al)2O60.1 wt%, SiO235.2 wt%, and 4.7 wt% of other substances, and has a particle diameter of 20 to 100 μm and an average particle diameter of 66 μm.
The heavy hydrocarbon oil feedstock used was a vacuum residue, the properties of which are shown in table 1.
The heavy hydrocarbon oil feed in Table 1 was preheated to a kinematic viscosity of 5mm2And/s, then contacting and reacting the preheated heavy hydrocarbon oil raw material and the coke transfer agent in the reaction unit, wherein the specific reaction conditions are shown in the table 2. The product oil gas obtained by the reaction is led out of the reaction unit through a pipeline and is separated from a coke transfer agent loaded with coke deposited carbon (wherein the coke content is 3 weight percent); the coke transfer agent of the coke deposit enters a gasifier of the regeneration unit to react with oxygen-containing gas (the specific reaction conditions are shown in Table 2), and the synthesis gas (effective gas (CO + H) is obtained after the reaction2) The content is more than 60 percent (dry basis)) is led out of the regeneration unit through a pipeline, the second gas (specifically water vapor) and the regenerant obtained after regeneration enter a solid particle size controller of a size control unit through a pipeline for separation, to obtain a large-particle regenerant (having a particle size of more than 80 μm and particles having a particle size of more than 100 μm accounting for 80 wt% of the whole of the large-particle regenerant), a medium-particle regenerant (having an average particle size of 63 μm) and a small-particle regenerant (having a particle size of less than 20 μm, and particles with the particle size of less than 10 mu m account for 75 wt% of the whole small particle regenerant), the small particle regenerant and the large particle regenerant are respectively led out of the reaction system through pipelines, and a medium particle size regenerant introduced into the reaction unit to be recycled as a coke transfer agent, wherein the conditions in the particle size controller comprise: the temperature was 510 ℃ and the pressure was 0.13 MPa.
And, the flow rates of the gases introduced into the first gas inlet, the second gas inlet and the third gas inlet are respectively listed in table 3.
The effect is as follows: in the contact agent in the reaction unit in the process of fluidized processing of the heavy oil, 20-80 mu m particles account for more than 90 wt% of the total particles in the reaction unit, and the stable operation period of the fluidized processing of the heavy oil is more than 1000 h.
Example 2
This example uses the same solid particle size controller as in example 1 to separate the regenerant during the fluidized processing of heavy oil and controls the following parameter conditions, while the rest of the parameter conditions are the same as in example 1:
large particle regenerant: the particle size is more than 80 μm, and the particles with the particle size of more than 100 μm account for 87 weight percent of the whole large particle regenerant;
medium particle size regenerant: the average particle size was 62 μm;
small particle regenerant: the particle size was less than 20 μm and the particles with a particle size of less than 10 μm accounted for 86 wt% of the total small particle regenerant.
The gas flow rates introduced by the first gas inlet, the second gas inlet and the third gas inlet are listed in table 3, respectively.
The effect is as follows: in the contact agent in the reaction unit in the process of fluidized processing of the heavy oil, 20-80 μm particles account for more than 94 weight percent of the total particles in the reaction unit, and the stable operation period of the fluidized processing of the heavy oil is more than 1000 h.
Comparative example 1
This comparative example was conducted in a similar manner to example 1 except that the regenerant in the fluidized heavy oil process was not separated using a solid particle size controller, but 80 wt% of the regenerant in the fluidized heavy oil process was directly recycled to the reaction unit as a coke transfer agent.
The remaining parameters during the fluidization of the heavy oil are the same as in example 1.
As a result: in the contact agent in the reaction unit in the process of heavy oil fluidization processing, 20-80 μm particles account for 70 wt% of the total particles in the reaction unit, and the stable operation period of the heavy oil fluidization processing is only 24 h.
TABLE 1
| Item | Vacuum residuum |
| Density (20 ℃ C.)/(g/cm)3) | 1.0387 |
| Kinematic viscosity/(mm)2/s) | |
| 80℃ | 2900 |
| 100℃ | 584 |
| Carbon residue/weight% | 26.8 |
| Four components/weight% | |
| Saturated hydrocarbons | 13.5 |
| Aromatic hydrocarbons | 38.2 |
| Glue | 27.5 |
| Asphaltenes | 20.8 |
| The element composition by weight percent | |
| C | 85.33 |
| H | 9.91 |
| S | 3.10 |
| N | 0.50 |
| Metal content/(μ g/g) | |
| Ni | 55 |
| V | 384 |
TABLE 2
| Reaction unit | |
| Temperature/. degree.C | 510 |
| pressure/kPa | 0.130 |
| Time/ |
2 |
| Weight ratio of coke transfer agent to heavy hydrocarbon oil feedstock | 7 |
| Weight ratio of steam to heavy hydrocarbon oil feedstock | 0.1:1 |
| Reproducing unit | |
| Temperature/. degree.C | 780 |
| Air velocity/m/s of empty bed | 0.5 |
| Time/s | 100 |
TABLE 3
From the above results, it can be seen that when the solid particle size controller provided by the present invention is applied to the process of fluidized processing of heavy oil, good fluidization can be achieved, uniformity of particle size of the contact agent particles in the reaction unit can be ensured, and long-term stable operation of the solid particles in the residual oil fluidized processing apparatus can be ensured.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.
Claims (20)
1. A solid particle size controller, the size controller comprising:
the first separation zone (A) is used for separating the large-particle regenerant and the medium-particle size regenerant, the first separation zone contains a separation unit (11) and a transmission unit (9) connected with the separation unit (11), the upper part of the separation unit is provided with a feed inlet (1), the lower part of the separation unit is provided with a first gas inlet (2), and the bottom of the separation unit is provided with a first discharge hole (8) for leading out the large-particle regenerant;
a second separation zone (B) for separating medium-size regenerant and small-size regenerant, wherein one end of the transfer unit (9) in the first separation zone (A) is embedded into the second separation zone (B), and the lower part of the second separation zone (B) is provided with a third gas inlet (4) and a second discharge hole (7) for leading out the medium-size regenerant; a baffle (10) is also arranged in the second separation zone (B) to enable a stream introduced into the second separation zone (B) from the top of the transfer unit (9) to flow towards the bottom of the second separation zone (B) after contacting the baffle; the top of the second separation area (B) is provided with a gas-solid separator (5) and a third discharge hole (6) for leading out the small particle regenerant.
2. The particle size controller according to claim 1, wherein a second gas inlet (3) is further provided in the transport unit (9) in the first separation zone (a).
3. The particle size controller according to claim 1 or 2, wherein a gas distributor is further arranged in the first separation zone (a) to enable the gas introduced by the first gas inlet (2) to move in the first separation zone (a) towards the transport unit (9).
4. The particle size controller according to claim 1 or 2, wherein a gas distributor is further provided in the second separation zone (B) to enable the gas introduced by the third gas inlet (4) to move in the second separation zone (B) towards the gas-solid separator (5).
5. The particle size controller according to any of claims 2-4, wherein the second gas inlet (3) is arranged in a direction such that gas introduced by the second gas inlet (3) is movable towards the second separation zone (B).
6. The particle size controller of any of claims 1-5, wherein the first separation zone (A) and the second separation zone (B) are coaxial with each other.
7. A particle size controller according to any of claims 1-6, wherein the length of the first separation zone (A) is 10-50% of the total length of the particle size controller, and the length of the first separation zone (A) is the distance between the bottom of the separation unit (11) and the top of the transport unit (9).
8. The particle size controller of any of claims 1-6, wherein the length of the second separation zone (B) is 50-90% of the total length of the particle size controller, and the length of the second separation zone (B) is the distance between the bottom of the second separation zone (B) and the top of the second separation zone (B).
9. The particle size controller according to any one of claims 1-6, wherein the separation unit (11) is a hollow reducing cylinder with a thick middle and thin ends.
10. Use of a solid particle size controller according to any one of claims 1 to 9 for separating solid particles.
11. A method of separating solid particles using the particle size controller of any one of claims 1-9, the method comprising: introducing gas into the particle size controller from a first gas inlet (2) and a third gas inlet (4) respectively and introducing solid particles from a feed inlet (1) into a separation unit (11) of a first separation zone (A), controlling the flow rate of gas introduced into the particle size controller from the first gas inlet (2) such that large particle solids of the solid particles are withdrawn from a first discharge outlet (8) and such that material containing medium and small particle solids moves upwardly from a transfer unit (9) into a second separation zone (B), and controlling the separation conditions of a gas-solids separator (5) and the flow rate of gas introduced into the particle size controller from the third gas inlet (4) such that the material containing medium and small particle solids separates the obtained medium and small particle solids in the second separation zone (B), the medium size solids are withdrawn from a second discharge (7) and the gas and the small particle solids are withdrawn from a third discharge (6).
12. The method of claim 11, wherein the method further comprises: introducing gas into the particle size controller from a second gas inlet (3).
13. The method of claim 11 or 12, wherein the solid particles are regenerants in the fluidized processing of heavy oils.
14. The method according to claim 13, wherein the flow rate of the gas introduced into the particle size controller from the first gas inlet (2) is controlled to be 0.01-0.8m/s, preferably 0.05-0.5 m/s.
15. The method according to claim 13, wherein the flow rate of the gas introduced into the particle size controller from the second gas inlet (3) is controlled to be 1-38m/s, preferably 2-18 m/s.
16. The method according to claim 13, wherein the flow rate of the gas introduced into the particle size controller from the third gas inlet (4) is controlled to be 0.01-0.8m/s, preferably 0.05-0.5 m/s.
17. The method according to any one of claims 13-16, wherein the flow rate of gas introduced from each gas inlet and the separation conditions of the gas-solid separator (5) are controlled such that the particle size of the large particle solids withdrawn from the first outlet (8) is greater than 80 μ ι η, wherein particles greater than 100 μ ι η comprise 50-95 wt.% of the total large particle solids withdrawn from the first outlet (8);
preferably, it is 60-95 wt% of the total large particle solids withdrawn from the first outlet (8).
18. A method according to any one of claims 13-16, wherein the flow rate of gas introduced from each gas inlet and the separation conditions of the gas-solid separator (5) are controlled such that the particle size of the small particle solids withdrawn from the third outlet (6) is less than 20 μm, wherein particles smaller than 10 μm constitute 50-95 wt.% of the total small particle solids withdrawn from the third outlet (6);
preferably, it represents 60-95% by weight of the total of said small particulate solids withdrawn from said third outlet (6).
19. A method according to any one of claims 13-16, wherein the flow rate of the gas introduced from each gas inlet and the separation conditions of the gas-solid separator (5) are controlled such that the average particle size of the medium-sized solids withdrawn from the second outlet (7) is 20-100 μm, preferably 40-80 μm.
20. The method of any of claims 13-16, wherein the conditions in the particle size controller comprise: the temperature is 350 ℃ and 900 ℃, and the pressure is 0.13-4 MPa.
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Citations (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1507715A1 (en) * | 1966-02-23 | 1969-04-03 | Miag Muehlenbau & Ind Gmbh | Method and device for the pneumatic sifting of bulk goods |
| WO1995022414A1 (en) * | 1994-02-16 | 1995-08-24 | Stripping Technologies, Inc. | Improved air-flow control for particle cleaning systems |
| JP2005199224A (en) * | 2004-01-19 | 2005-07-28 | National Institute Of Advanced Industrial & Technology | Wind power screening device |
| CN1935349A (en) * | 2005-09-23 | 2007-03-28 | 中国石油大学(北京) | Gas-solid fluidized coupling equipment and coupling method for particle mixing-classifying by utilizing same |
| CN1990098A (en) * | 2005-12-20 | 2007-07-04 | 法国石油公司 | Reactor comprising two fluidised reaction zones and an integrated gas/solid separation system |
| CN100998979A (en) * | 2006-01-09 | 2007-07-18 | 同济大学 | Multi-lateral-line solid fluidization pneumatic transfer separation device and method of printed circuit board |
| JP4122438B2 (en) * | 2004-01-21 | 2008-07-23 | 独立行政法人産業技術総合研究所 | Multistage wind sorter |
| CN102716857A (en) * | 2012-06-08 | 2012-10-10 | 清华大学 | Pneumatic particle size classifying device for solid particles |
| CN102935428A (en) * | 2012-11-08 | 2013-02-20 | 品孚罗特过滤设备（北京）有限公司 | Device for separating solid particles and application thereof |
| CN103831245A (en) * | 2013-11-21 | 2014-06-04 | 宿迁市现代生物科技有限公司 | Curved-way-type rotator-free airflow grader used for fine particle materials |
| CN104271267A (en) * | 2012-03-28 | 2015-01-07 | 独立行政法人产业技术综合研究所 | Particle sorting machine |
| CN104475341A (en) * | 2014-10-24 | 2015-04-01 | 袁志刚 | Single-unit pneumatic centrifugal powder classification device for separating four particle size specifications |
| CN205341286U (en) * | 2016-02-25 | 2016-06-29 | 神华集团有限责任公司 | Solid mixture's piece -rate system |
| CN205463188U (en) * | 2016-01-22 | 2016-08-17 | 中国矿业大学 | Electronic waste air current sorting unit in experiment teaching |
| CN106269508A (en) * | 2016-09-08 | 2017-01-04 | 清华大学 | A kind of annular fluidized bed separator of granulate mixture |
| CN108465563A (en) * | 2017-02-23 | 2018-08-31 | 中国石油化工股份有限公司 | Solid material dry separation device and method |
-
2018
- 2018-12-07 CN CN201811495644.7A patent/CN111282815B/en active Active
Patent Citations (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1507715A1 (en) * | 1966-02-23 | 1969-04-03 | Miag Muehlenbau & Ind Gmbh | Method and device for the pneumatic sifting of bulk goods |
| WO1995022414A1 (en) * | 1994-02-16 | 1995-08-24 | Stripping Technologies, Inc. | Improved air-flow control for particle cleaning systems |
| JP2005199224A (en) * | 2004-01-19 | 2005-07-28 | National Institute Of Advanced Industrial & Technology | Wind power screening device |
| JP4122438B2 (en) * | 2004-01-21 | 2008-07-23 | 独立行政法人産業技術総合研究所 | Multistage wind sorter |
| CN1935349A (en) * | 2005-09-23 | 2007-03-28 | 中国石油大学(北京) | Gas-solid fluidized coupling equipment and coupling method for particle mixing-classifying by utilizing same |
| CN1990098A (en) * | 2005-12-20 | 2007-07-04 | 法国石油公司 | Reactor comprising two fluidised reaction zones and an integrated gas/solid separation system |
| CN100998979A (en) * | 2006-01-09 | 2007-07-18 | 同济大学 | Multi-lateral-line solid fluidization pneumatic transfer separation device and method of printed circuit board |
| CN104271267A (en) * | 2012-03-28 | 2015-01-07 | 独立行政法人产业技术综合研究所 | Particle sorting machine |
| CN102716857A (en) * | 2012-06-08 | 2012-10-10 | 清华大学 | Pneumatic particle size classifying device for solid particles |
| CN102935428A (en) * | 2012-11-08 | 2013-02-20 | 品孚罗特过滤设备（北京）有限公司 | Device for separating solid particles and application thereof |
| CN103831245A (en) * | 2013-11-21 | 2014-06-04 | 宿迁市现代生物科技有限公司 | Curved-way-type rotator-free airflow grader used for fine particle materials |
| CN104475341A (en) * | 2014-10-24 | 2015-04-01 | 袁志刚 | Single-unit pneumatic centrifugal powder classification device for separating four particle size specifications |
| CN205463188U (en) * | 2016-01-22 | 2016-08-17 | 中国矿业大学 | Electronic waste air current sorting unit in experiment teaching |
| CN205341286U (en) * | 2016-02-25 | 2016-06-29 | 神华集团有限责任公司 | Solid mixture's piece -rate system |
| CN106269508A (en) * | 2016-09-08 | 2017-01-04 | 清华大学 | A kind of annular fluidized bed separator of granulate mixture |
| CN108465563A (en) * | 2017-02-23 | 2018-08-31 | 中国石油化工股份有限公司 | Solid material dry separation device and method |
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|---|---|
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