CN110903848A - Device and method for co-converting heavy inferior oil and coal - Google Patents

Abstract

The invention discloses a device and a method for high-efficiency co-conversion of heavy inferior oil and coal, wherein the device comprises a feeding unit, a gasification unit, a cracking unit and a coke breeze return unit; the feeding unit comprises a raw oil feeding system and a coal powder feeding system, and the stable conveying of the raw oil and the coal powder is completed; the gasification unit comprises a gasification zone, a gasification separator and a particle reflux device, and the gasification of the semicoke and the coal is completed; the cracking unit comprises a premixing area and a lifting cracking area, and the co-cracking of the raw oil and the solid medium is completed; the fine coke returning unit comprises a cracking separator, a pressure swing collection tank, a secondary pressure swing buffer tank, a semicoke collection tank and a semicoke feeder, and is used for completing gas-solid separation and material returning of a gasification zone and a cracking zone of solid semicoke; the invention effectively overcomes the defects of low petroleum coke yield and limited heat supply in the single cracking of the heavy and inferior oil, provides the heat carrier and the hydrogen-rich reaction gas, effectively improves the coking problem caused by the side wall effect in the cracking process of the heavy and inferior oil, and improves the yield and the quality of the cracked oil.

Description

Device and method for co-converting heavy inferior oil and coal

Technical Field

The invention belongs to the technical field of coal chemical industry, and particularly relates to a device and a method for co-converting heavy inferior oil and coal.

Background

With the heavy and inferior crude oil, the yield of inferior heavy oil or residual oil (heavy oil, super heavy oil, oil sand bitumen, vacuum residual oil, deoiled bitumen, etc., hereinafter referred to as inferior heavy oil) increases dramatically. The upgrading technology of inferior heavy oil can be divided into two routes of decarburization and hydrogenation, which mainly comprise delayed coking, hydrocracking, catalytic cracking and the like. Due to the problems of catalyst deactivation, operation cost, technical maturity and the like, the catalytic processing process represented by catalytic cracking and hydrocracking is difficult to meet the treatment requirement of inferior heavy oil. The delayed coking process produces a large amount of coke, particularly high-sulfur petroleum coke, and has a large outgoing problem, the high-sulfur coke with the sulfur content of more than 3 percent is regulated by the atmospheric pollution prevention and treatment law of the people's republic of China issued in 2015, 8 and 29, and the coking process needs to be transformed urgently. The direct single gasification process directly converts heavy oil into small molecules such as synthesis gas and the like, oil gas molecules and hydrogen elements existing in the heavy oil are not fully utilized, and heavy oil resource waste is caused to a certain extent. Therefore, a novel heavy and inferior oil processing technology which can adapt to heavy and inferior oil processing, has high energy conversion efficiency, high oil product yield and large processing scale is urgently needed.

The heavy inferior oil cracking process is easy to coke, the quantity of petroleum coke generated is small, the key is how to avoid the reaction coking of the heavy inferior oil, and the pyrolysis gasification integrated reaction of the single heavy inferior oil is difficult to realize. The coal gasification can generate hydrogen-rich synthetic gas and generate 70% of semicoke, if the generated synthetic gas and the semicoke can participate in the cracking reaction process of the heavy inferior oil, the fluidized gas and the heat carrier can be provided for cracking the heavy inferior oil, the dispersion density of the heavy inferior oil can be reduced, the possibility of coking is reduced, and the side wall effect in the cracking process of the heavy inferior oil is effectively improved.

Disclosure of Invention

In order to overcome the defects of the prior art, the invention aims to provide a device and a method for high-efficiency co-conversion of heavy inferior oil and coal, which improve the side wall effect in the cracking process of the heavy inferior oil and improve the quality and the yield of the cracked oil.

In order to achieve the purpose, the invention adopts the following technical scheme:

the utility model provides a device of heavy inferior oil and high-efficient cotransformation of coal, includes feed unit, gasification unit, schizolysis unit, fine coke feed back unit:

the feeding unit comprises a raw oil feeding system and a coal powder feeding system: the raw oil feeding system comprises a raw oil preheater communicated with raw oil and an efficient atomizer communicated with the outlet of the raw oil preheater, and the raw oil preheated by the raw oil preheater is mixed with steam and atomized in the efficient atomizer; the pulverized coal feeding system comprises a coal hopper, a coal feeding lock hopper, a feeding hopper and a fluidized feeder, wherein the coal feeding lock hopper is sequentially communicated with the coal hopper from the discharging direction of the coal hopper;

the cracking unit comprises a premixing area and a lifting cracking area which is arranged at the top of the premixing area and communicated with the premixing area, and the premixing area is communicated with an outlet of a high-efficiency atomizer in the raw oil feeding system;

the gasification unit comprises a gasification area which is arranged at the bottom of the premixing area and is communicated with the outlet of the fluidization feeder and provided with an ash discharge port, a pipe mixer communicated with the gasification area, a particle reflux device with a top inlet communicated with the premixing area and a bottom outlet communicated with the gasification area, and a gasification separator with a top gas outlet communicated with the premixing area and a bottom solid outlet communicated with the gasification area, wherein the inlet of the gasification separator is communicated with the gasification area;

the fine coke return unit comprises a cracking separator communicated with an outlet of a lifting cracking area, an outlet at the top of the cracking separator is connected with a subsequent purification and separation system, a variable pressure collecting tank, a secondary variable pressure buffer tank, a semi-coke collecting tank and a semi-coke feeder are sequentially communicated at the bottom of the cracking separator from a fine coke return direction, wherein an inlet of the secondary variable pressure buffer tank is communicated with an outlet of a coal feeding lock hopper in a pulverized coal feeding system, and an outlet of the semi-coke feeder is communicated with a gasification area and a lifting cracking area.

Furthermore, the raw materials for cracking in the lifting cracking zone are heavy inferior oil and coal, and the raw materials for gasification in the gasification zone are petroleum coke, semicoke and coal.

Further, the heavy inferior oil comprises heavy oil with carbon residue of more than 20%, super heavy oil, oil sand asphalt, vacuum residue oil and deoiled asphalt.

Furthermore, the gasification separator can capture semicoke particles with the solid particle size larger than 100 μm, the cracking separator can capture semicoke particles with the solid particle size larger than 50 μm, and the gas after separation by the cracking separator carries a small amount of fine semicoke powder to continue subsequent purification and separation.

Further, the loosening air quantity of the particle reflux device can be adjusted.

Further, the diameter of the premixing area is 2-5 times of that of the lifting cracking area.

The method for carrying out the high-efficiency co-conversion of the heavy inferior oil and the coal by utilizing the device comprises the following steps:

the method comprises the following steps: coal is added into a coal hopper, the coal sequentially passes through a coal feeding lock hopper, a feeding hopper and a fluidized feeder to enter a gasification zone, gasification agent oxygen/air and steam are introduced into the bottom of the gasification zone through a pipe mixer, the coal is gasified in the gasification zone, and generated hydrogen-rich synthesis gas carries generated semicoke solid particles to enter a premixing zone through an outlet at the top of a gasification separator;

step two: raw oil is introduced into a raw oil preheater for preheating, steam is introduced into a high-efficiency atomizer to atomize the preheated raw oil, the atomized raw oil enters a premixing area and is rapidly mixed with hydrogen-rich synthesis gas carrying solid particles to form a mixture so as to reduce the dispersion density of the oil particles, the purpose of rapid heat exchange is achieved, the solid semicoke particles in the premixing area flow back to a gasification area through a particle reflux device to participate in subsequent reaction, the mixture enters a lifting cracking area through the premixing area and is instantly mixed with semicoke powder conveyed by a semicoke returning unit semicoke feeder and passes through the lifting cracking area to form oil gas and solid semicoke through a cracking separator, the oil gas enters a subsequent purification and separation system, and the solid semicoke enters the gasification area or the lifting cracking area through a semicoke returning unit to participate in reaction.

Further, the preheating temperature of the raw oil is 130-180 ℃, the retention time of the raw oil in the premixing area and the enhanced cracking area is 10-20s, and the agent-oil ratio is 4: 10.

further, the reaction temperature of the gasification zone is 800-.

Further, the fluidizing medium used at the initial temperature rise of the system is one or more combinations of inert particles, spent catalyst, and carbonaceous particles.

Compared with the prior art, the invention has the following beneficial effects:

raw oil is introduced through a raw oil feeding system of a feeding unit and atomized and enters a premixing area to be rapidly mixed with hydrogen-rich synthesis gas which is introduced from a pipe mixer and carries solid particles, oxygen/air and steam are synthesized in a gasification area, the dispersion density of the oil particles is reduced, and the purpose of rapid heat exchange is achieved. Because the inlet of the secondary pressure swing buffer tank is communicated with the outlet of the coal feeding lock hopper in the pulverized coal feeding system, namely the pulverized coke returning unit is communicated with the pulverized coal feeding system, coal can directly enter a lifting cracking zone to be subjected to cotransformation reaction with heavy inferior oil, and the defects that the yield of petroleum coke cracked by the heavy inferior oil alone is low and the heat supply is limited are effectively overcome; meanwhile, the invention conveys the hydrogen-rich synthesis gas carrying solid particles generated by coal gasification in the gasification zone to the premixing zone through the gasification separator, so that the hydrogen-rich synthesis gas participates in the subsequent crude oil cracking reaction, provides a heat carrier and the hydrogen-rich reaction gas for the subsequent crude oil cracking reaction, effectively improves the side wall effect in the heavy and inferior oil cracking process and improves the quality and yield of the cracked oil.

Furthermore, the gasification separator can effectively prevent the larger semicoke particles from entering a subsequent device by collecting the semicoke particles with the solid particle size larger than 100 mu m and the cracking separator can effectively prevent the larger semicoke particles from entering the subsequent device by collecting the semicoke particles with the solid particle size larger than 50 mu m, so that the reduction of the system conversion reaction efficiency and the adverse effect on a subsequent purification and separation system caused by the larger semicoke particles are avoided.

Furthermore, the diameter of the premixing area is 2-5 times of that of the cracking area, so that the process that the raw oil flows into the cracking area from the premixing area is a rapid speed-up stage, the solid particle circulation rate is high, the side wall effect of heavy oil cracking is further weakened, and the possibility of oil cracking and coking is further reduced.

Drawings

Fig. 1 is an overall structural view of the present invention.

In the figure: 1. a gasification zone; 2. a pre-mixing zone; 3. lifting the cracking zone; 4. a high efficiency atomizer; 5. a coal hopper; 6. locking the hopper for coal feeding; 7. a coal hopper; 8. a pulverized coal feeder; 9. a pipe mixer; 10. a gasification separator; 11. a particle reflux vessel; 12. a pyrolysis separator; 13. a pressure swing collection tank; 14. a secondary pressure-changing buffer tank; 15. a semicoke collection tank; 16. a semicoke feeder; 17. an ash discharge port; 18. a raw oil preheater.

Detailed Description

The invention is described in further detail below with reference to specific embodiments and with reference to the following drawings.

Referring to fig. 1, the device of the invention comprises a feeding unit, a gasification unit, a cracking unit and a coke breeze returning unit;

the feeding unit is used for stably conveying raw oil and coal powder, the raw oil is heavy inferior oil, and the feeding unit comprises a raw oil feeding system and a coal powder feeding system: the raw oil feeding system comprises a raw oil preheater 18, wherein an inlet of the raw oil preheater 18 is communicated with raw oil, the raw oil is heavy inferior oil comprising thickened oil with carbon residue of more than 20%, super-thickened oil, oil sand asphalt, vacuum residual oil and deoiled asphalt, an outlet of the raw oil preheater 18 is communicated with an inlet of the efficient atomizer 4, and the raw oil preheated by the raw oil preheater 18 is mixed with steam and atomized in the efficient atomizer 4; the pulverized coal feeding system comprises a coal hopper 5, a coal feeding lock hopper 6, a feeding hopper 7 and a fluidized feeder 8, wherein the coal hopper 5 is arranged at the uppermost part of the pulverized coal feeding system, coal added into the coal hopper 5 is discharged from top to bottom, and a lower outlet of the coal hopper 5 is sequentially communicated with the coal feeding lock hopper 6, the feeding hopper 7 and the fluidized feeder 8 according to the discharging direction;

the cracking unit is used for completing the co-cracking of raw oil and a solid medium, and comprises a premixing area 2 communicated with an outlet of a high-efficiency atomizer 4 in a raw oil feeding system, and a lifting cracking area 3 arranged at the top of the premixing area 2 and communicated with the premixing area, wherein heavy inferior oil and coal are used as raw materials for cracking, and the diameter of the premixing area is set to be 2-5 times of the diameter of the lifting cracking area in order to realize the rapid high-rate circulation of solid particles flowing into the lifting cracking area from the premixing area, further weaken the side wall effect of heavy oil cracking and further reduce the possibility of oil cracking coking;

the gasification unit is used for completing gasification of semicoke and coal and comprises a gasification zone 1, a pipe mixer 9, a particle reflux device 11 and a gasification separator 10, wherein the gasification zone 1 is arranged at the bottom of a premixing zone 2 and is communicated with an outlet of a fluidization feeder 8, raw materials gasified in the gasification zone 1 are petroleum coke, semicoke and coal, the gasification zone 1 is also provided with an ash discharge port 17 for discharging ash, the pipe mixer 9 is communicated with the gasification zone 1, gasification agent oxygen/air and steam introduced from the pipe mixer 9 enter the gasification zone 1, a top inlet of the particle reflux device 11 is communicated with the premixing zone 2, a bottom outlet is communicated with the gasification zone 1, the loosening gas amount of the particle reflux device 11 can be adjusted so as to control the conveying of solid coke particles in the premixing zone to the gasification zone, a top gas outlet of the gasification separator 10 is communicated with the premixing zone 2, and a bottom solid outlet is communicated with the gasification zone 1, the inlet of the gasification separator 10 is communicated with the gasification zone 1, the hydrogen-rich synthesis gas carrying solid semicoke particles generated in the gasification zone 1 enters from the inlet of the gasification separator 10 and is separated by the gasification separator 10, in order to prevent the larger semicoke particles from entering a subsequent device and avoid the phenomenon that the larger semicoke particles cause the reduction of the conversion reaction efficiency of the system, the semicoke particles with the diameter larger than 100 μm which can be collected by the gasification separator 10 enter the gasification zone again for gasification after being separated by the gasification separator 10, the separated gas carries the solid semicoke particles with small diameter as a heat carrier and fluidized gas to enter the premixing zone 2, the synthesis gas is in hydrogen-rich atmosphere, and the quality and yield of the pyrolysis oil can be effectively improved;

the fine coke return unit is used for completing gas-solid separation and gasification area and cracking area return of solid semicoke, and comprises a cracking separator 12, a pressure swing collection tank 13, a secondary pressure swing buffer tank 14, a semicoke collection tank 15 and a semicoke feeder 16, wherein an inlet of the cracking separator 12 is communicated with an outlet of a lifting cracking area 3, the cracking separator 12 is used for separating oil gas and solid semicoke, the oil gas enters a subsequent purification and separation system through a top outlet of the cracking separator 12, in order to prevent larger semicoke particles from entering the subsequent device and avoid adverse effects on the subsequent purification and separation system, the cracking separator 12 can capture semicoke particles with the particle size larger than 50 mu m, the solid semicoke flows from top to bottom in the cracking separator 12 to an outlet of the cracking separator 12, and a bottom outlet of the cracking separator 12 is sequentially communicated with the pressure swing collection tank 13 from the discharge direction of the solid semicoke, Second grade vary voltage buffer tank 14, semicoke collection tank 15, semicoke feeder 16, second grade vary voltage buffer tank 14's pressure is adjustable, with this make the fine coke returning charge unit possess the effect that gas-solid separation and fine coke were carried simultaneously, semicoke feeder 16's export and gasification district 1, promote pyrolysis zone 3 homogeneous phase intercommunication, second grade vary voltage buffer tank 14's entry still with in the fine coal charge system export intercommunication of giving coal lock fill 6, with this make fine coal charge system and fine coke returning charge unit intercommunication, the coal can be followed the selection after the coal charge system joining and got into promotion pyrolysis zone 3 or gasification district 1.

The method for efficiently co-converting the heavy inferior oil and the coal by using the device comprises the following specific steps:

the method comprises the following steps: the system pressure of the control device is 0.1MPa-1.0MPa, coal is added into a coal hopper 5, the coal sequentially passes through a coal feeding lock hopper 6, a feeding hopper 7 and a fluidization feeder 8 to enter a gasification zone 1, meanwhile, gasifying agent oxygen/air and steam are introduced into the bottom of the gasification zone 1 through a pipe mixer 9, the reaction temperature of the gasification zone 1 is controlled to be 800-;

step two: raw oil is fed into a raw oil preheater 18 to be preheated to 130-20 seconds, steam is fed into a high-efficiency atomizer 4 to atomize the preheated raw oil, the atomized raw oil enters a premixing zone 2 to be rapidly mixed with hydrogen-rich synthesis gas carrying solid particles to form a mixture so as to reduce the dispersion density of the oil particles, the purpose of rapid heat exchange is achieved, the solid semicoke particles in the premixing zone 2 flow back to a gasification zone 1 through a particle reflux device 11 to participate in subsequent reaction, the mixture enters a lifting cracking zone 3 through the premixing zone 2 to be instantly mixed with semicoke powder conveyed by a semicoke returning unit semicoke feeder 16, the temperature of the lifting cracking zone 3 is controlled to 400-700 seconds through the lifting cracking zone 3, the retention time of the raw oil in the premixing zone and the lifting cracking zone is 10-20 seconds, and the oil-to-oil ratio is 4: 10, the raw oil leaves the lifting cracking zone 3 and then passes through a cracking separator 12 to form oil gas and solid semicoke, the oil gas enters a subsequent purification and separation system, and the solid semicoke enters the gasification zone 1 or the lifting cracking zone 3 through a coke breeze return unit to participate in reaction.

The working process of the device of the invention is as follows:

coal is added through a coal hopper 5 of a pulverized coal feeding system, flows through a coal feeding lock hopper 6, a feeding hopper 7 and a fluidized feeder 8 to a gasification zone 1 in sequence, is mixed with gasifying agent oxygen/air and steam flowing into the gasification zone 1 through a pipe mixer 9 and is gasified to generate semicoke and hydrogen-rich synthetic gas through gasification, the hydrogen-rich synthetic gas carries solid semicoke particles to flow from an outlet of the gasification zone 1 to a gasification separator 10, the gasification separator 10 returns the separated large-particle solid semicoke to the gasification zone 1 from a solid outlet at the bottom thereof to participate in the co-gasification of the coal and the semicoke, the separated small-particle solid semicoke and the hydrogen-rich synthetic gas are transmitted to a premixing zone 2 from a gas outlet at the top thereof, at the moment, raw oil which is preheated by a raw oil preheater 18 and atomized by a high-efficiency atomizer 4 flows into the premixing zone 2 to be rapidly mixed with the particle solid semicoke and the hydrogen-rich synthetic gas, the dispersion density of oil particles is reduced to achieve the purpose of rapid heat exchange, the mixed oil particles enter a lifting cracking zone 3 through a premixing zone 2, in the actual operation, the loosening air quantity of a particle reflux device 11 can be adjusted, so that solid semicoke particles in the premixing zone 2 flow back to a gasification zone 1 through the particle reflux device 11 to continuously participate in the co-gasification of coal and semicoke, at the moment, coal added into a coal hopper 5 of a coal powder feeding system flows out of a coal feeding lock hopper 6, a secondary variable pressure buffer tank 14, a semicoke collecting tank 15 and a semicoke feeder 16 to the lifting cracking zone 3, so that the coal and raw oil are jointly cracked and efficiently converted, the cracked and converted coal and raw oil flow to a cracking separator 12 and are separated by the cracking separator 12 to form oil gas and solid semicoke, the oil gas enters a subsequent purification and separation system, and the solid semicoke passes through a variable pressure collecting tank 13, a secondary variable pressure buffer tank 14, a fine coke returning unit, The semicoke collecting tank 15 and the semicoke feeder 16 enter the gasification zone 1 to participate in co-gasification or enter the lifting cracking zone 3 to participate in co-cracking conversion of coal and heavy inferior oil.

Claims (10)

1. The device for high-efficiency co-conversion of the heavy inferior oil and the coal is characterized by comprising a feeding unit, a gasification unit, a cracking unit and a coke breeze returning unit;

the feeding unit comprises a raw oil feeding system and a coal powder feeding system: the raw oil feeding system comprises a raw oil preheater (18) communicated with raw oil and an efficient atomizer (4) communicated with an outlet of the raw oil preheater (18), and the raw oil preheated by the raw oil preheater (18) is mixed with steam and atomized in the efficient atomizer (4); the pulverized coal feeding system comprises a coal hopper (5), a coal feeding lock hopper (6), a feeding hopper (7) and a fluidized feeder (8), wherein the coal feeding lock hopper is sequentially communicated with the coal hopper (5) from the discharging direction of the coal hopper (5);

the cracking unit comprises a premixing area (2) and a lifting cracking area (3) which is arranged at the top of the premixing area (2) and communicated with the premixing area, and the premixing area (2) is communicated with an outlet of a high-efficiency atomizer (4) in the raw oil feeding system;

the gasification unit comprises a gasification area (1) which is arranged at the bottom of the premixing area (2) and is communicated with the outlet of the fluidization feeder (8) and is provided with an ash discharge port (17), a pipe mixer (9) communicated with the gasification area (1), a particle reflux device (11) with a top inlet communicated with the premixing area (2) and a bottom outlet communicated with the gasification area (1), a gasification separator (10) with a top gas outlet communicated with the premixing area (2) and a bottom solid outlet communicated with the gasification area (1), wherein the inlet of the gasification separator (10) is communicated with the gasification area (1);

the fine coke return unit comprises a cracking separator (12) communicated with an outlet of a lifting cracking area (3), the top outlet of the cracking separator (12) is connected with a subsequent purification and separation system, the bottom of the cracking separator is sequentially communicated with a pressure-variable collecting tank (13), a secondary pressure-variable buffer tank (14), a semicoke collecting tank (15) and a semicoke feeder (16) through a fine coke return direction, wherein the inlet of the secondary pressure-variable buffer tank (14) is communicated with the outlet of a coal feeding lock hopper (6) in a pulverized coal feeding system, and the outlet of the semicoke feeder (16) is communicated with a gasification area (1) and the lifting cracking area (3).

2. The apparatus for high-efficiency co-conversion of heavy inferior oil and coal according to claim 1, wherein: the raw materials for cracking in the lifting cracking zone (3) are heavy inferior oil and coal, and the raw materials for gasification in the gasification zone (1) are petroleum coke, semicoke and coal.

3. The apparatus for high-efficiency co-conversion of heavy inferior oil and coal according to claim 2, wherein: the heavy inferior oil comprises heavy oil with carbon residue of more than 20%, super heavy oil, oil sand asphalt, vacuum residue oil and deoiled asphalt.

4. The apparatus for high-efficiency co-conversion of heavy inferior oil and coal according to claim 1, wherein: the gasification separator (10) can capture semicoke particles with solid particle size larger than 100 μm, the cracking separator (12) can capture semicoke particles with solid particle size larger than 50 μm, and gas after separation by the cracking separator carries a small amount of fine semicoke powder to continue subsequent purification and separation.

5. The apparatus for high-efficiency co-conversion of heavy inferior oil and coal according to claim 1, wherein: the loosening air quantity of the particle reflux device (11) can be adjusted.

6. The apparatus for high-efficiency co-conversion of heavy inferior oil and coal according to claim 1, wherein: the diameter of the premixing area (2) is 2-5 times of that of the lifting cracking area (3).

7. The method for efficiently co-converting the heavy inferior oil and the coal by using the device is characterized by comprising the following steps:

the method comprises the following steps: coal is added into a coal hopper (5), the coal enters a gasification zone (1) through a coal feeding lock hopper (6), a feeding hopper (7) and a fluidized feeder (8) in sequence, gasification agent oxygen/air and steam are introduced into the bottom of the gasification zone (1) through a pipe mixer (9), the coal is gasified in the gasification zone (1), and generated hydrogen-rich synthesis gas carries generated semicoke solid particles to enter a premixing zone (2) through an outlet at the top of a gasification separator (10);

step two: the method comprises the steps of introducing raw oil into a raw oil preheater (18) to preheat to 130-.

8. The method for high-efficiency co-conversion of heavy inferior oil and coal according to claim 7, characterized in that: the preheating temperature of the raw oil is 130-180 ℃, the retention time of the raw oil in the premixing zone (2) and the lifting cracking zone (3) is 10-20s, and the ratio of the raw oil to the catalyst is 4: 10.

9. the method for high-efficiency co-conversion of heavy inferior oil and coal according to claim 7, characterized in that: the reaction temperature of the gasification zone (1) is 800-.

10. The method for high-efficiency co-conversion of heavy inferior oil and coal according to claim 7, characterized in that: the fluidizing medium used at the initial temperature rise of the system is one or more combinations of inert particles, spent catalyst, and carbonaceous particles.

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