CN109306272B

CN109306272B - Heavy oil hydrotreating system

Info

Publication number: CN109306272B
Application number: CN201710627354.2A
Authority: CN
Inventors: 郑莹; 张其凯; 徐鹏辉
Original assignee: Jiechuang Dongying Energy Technology Co ltd
Current assignee: Jiechuang Dongying Energy Technology Co ltd
Priority date: 2017-07-27
Filing date: 2017-07-27
Publication date: 2022-04-26
Anticipated expiration: 2037-07-27
Also published as: CN109306272A

Abstract

The invention provides a heavy oil hydrotreating system, which comprises a main reactor and at least one sub-reactor, wherein the main reactor comprises a first cylinder, the first cylinder is used for containing materials, and the sub-reactor comprises: the mixing unit is used for mixing the material and the hydrogen, and comprises a second cylinder body, wherein the second cylinder body is provided with a material inlet, a hydrogen inlet and a first outlet, and the material inlet is communicated with the outlet of the first cylinder body; and the inlet of the strengthening device is communicated with the first outlet of the second cylinder, the outlet of the strengthening device is communicated with the accommodating cavity of the first cylinder, and the strengthening device is used for providing energy for the materials so as to enable the materials to generate a cracking reaction. By adopting the technical scheme provided by the invention, the problems of high operation cost and high investment cost of a heavy oil hydrotreating system in the prior art can be solved.

Description

Heavy oil hydrotreating system

Technical Field

The invention relates to the technical field of petrochemical industry, in particular to a heavy oil hydrotreating system.

Background

Heavy oil is the portion of crude oil remaining after the distillate oil is extracted. Compared with crude oil, the heavy oil has complex components, high density, high viscosity, large average molecular weight, low hydrogen-carbon ratio, high carbon residue value, and contains a large amount of harmful substances such as metal, sulfur, nitrogen, etc. Heavy oil needs to be treated from the viewpoint of energy utilization or environmental protection.

The crude oil is divided into light crude oil and heavy crude oil, along with the deepening of the oil exploitation degree, the components of the crude oil are heavier and heavier, and the phenomena of heavy crude oil and deterioration of the crude oil are more and more prominent, namely the proportion of the heavy crude oil is higher and higher. The heavy oil is difficult to process, and especially after the heavy crude oil is processed, the amount of the produced heavy oil may account for more than half of the total amount of the heavy crude oil, and the content of saturated hydrocarbon of the heavy oil is low, so that the subsequent processing is more difficult.

When heavy oil is treated, two technologies, namely a decarburization treatment process and a hydrogenation treatment process, are mainly included. In order to increase the utilization of heavy oil, a hydrotreating process may be employed. The hydrogenation process is to add hydrogen gas into heavy oil, and under the action of certain temperature, pressure and catalyst, the hydrogen ion and carbon ion are combined to saturate olefin and even arene so as to reach the aim of lightening. The existing heavy oil hydrotreating system adopting the hydrotreating process needs to operate under the conditions of high temperature and high pressure, and has large consumption of hydrogen, so that the operation cost of the heavy oil hydrotreating system is high. Moreover, since the heavy oil hydrotreating system needs to operate under high temperature and high pressure conditions, the system has high performance requirements, and the system has a complex structure, so that the investment cost of the heavy oil hydrotreating system is high.

Disclosure of Invention

The invention provides a heavy oil hydrotreating system, which aims to solve the problems of high operation cost and high investment cost of the heavy oil hydrotreating system in the prior art.

In order to solve the above problems, the present invention provides a heavy oil hydroprocessing system including a main reactor including a first barrel, and at least one sub-reactor including: the mixing unit is used for mixing the material and the hydrogen, and comprises a second cylinder body, wherein the second cylinder body is provided with a material inlet, a hydrogen inlet and a first outlet, and the material inlet is communicated with the outlet of the first cylinder body; and the inlet of the strengthening device is communicated with the first outlet of the second cylinder, the outlet of the strengthening device is communicated with the accommodating cavity of the first cylinder, and the strengthening device is used for providing energy for the materials so as to enable the materials to generate a cracking reaction.

Further, the strengthening device comprises a strengthening unit, the strengthening unit is one or more of a plasma unit, a cavitation unit, a stirring unit and an impact unit, the plasma unit is used for ionizing materials, the cavitation unit is used for enabling the materials to generate cavitation, the stirring unit is used for stirring the materials, and the impact unit is used for impacting the materials entering the accommodating cavity of the first cylinder.

Further, the strengthening device comprises a plurality of strengthening units, each strengthening unit is one of a plasma unit, a cavitation unit, a stirring unit and an impact unit, when one strengthening unit is the impact unit, an outlet of the impact unit is communicated with the accommodating cavity of the first cylinder, and the first outlet of the second cylinder, other strengthening units and the impact unit are communicated in sequence.

Further, the strengthening device comprises a plurality of strengthening units, each strengthening unit is one of a plasma unit, a cavitation unit and a stirring unit, and the first outlet of the second cylinder, the strengthening units and the accommodating cavity of the first cylinder are communicated in sequence.

Further, the plasma unit includes: the third cylinder body is provided with a first cylinder wall and a second cylinder wall, the first cylinder wall is arranged on the inner side of the second cylinder wall, a first cavity is arranged between the first cylinder wall and the second cylinder wall, a second cavity is arranged in the first cylinder wall, and materials can flow in the first cavity; a dielectric disposed in the second cavity; and the electrode at least partially penetrates into the dielectric, and one end of the electrode is connected with a high-voltage power supply.

Further, the cavitation unit includes: a fourth cylinder; the cavitation plate group is arranged in the fourth cylinder; and/or a cavitation nozzle disposed within the fourth barrel.

Further, the cavitation unit includes a cavitation plate group, and the cavitation plate group includes: the first plate body is provided with a plurality of through holes; the second plate body is provided with a plurality of through holes, and an included angle is formed between the second plate body and the first plate body.

Further, at least a portion of the first plate body has a serrated periphery, and/or at least a portion of the second plate body has a serrated periphery.

Furthermore, the number of the cavitation plate groups is multiple, and the multiple cavitation plate groups are sequentially arranged in the fourth cylinder body along the flowing direction of the material.

Further, the stirring unit includes: a fifth cylinder; the rotating shaft is rotatably arranged in the fifth cylinder, and the axial direction of the rotating shaft is arranged along the flowing direction of the materials; the paddles are arranged on the rotating shaft at intervals along the circumferential direction of the rotating shaft.

Further, the stirring unit further includes: and the arc-shaped baffles are fixedly arranged between the fifth cylinder and the paddles and are arranged at intervals along the circumferential direction of the rotating shaft.

Further, a striking unit is provided at an upper portion of the receiving chamber of the first cylinder, the striking unit including: the bracket is fixed on the inner side wall of the first cylinder; the conveying pipe is fixed on the support, and an inlet of the conveying pipe is communicated with the first outlet of the second cylinder.

Further, the strengthening device of the sub-reactor comprises an impact unit, an inlet of the impact unit is communicated with the first outlet of the second cylinder, and an outlet of the impact unit is communicated with the accommodating cavity of the first cylinder; the number of the sub-reactors is at least two, the outlets of the impact units of the at least two sub-reactors are arranged at intervals, and materials entering the first barrel from different impact units are impacted.

Further, the cross-sectional area of the inner wall of the second cylinder is larger than that of the inner wall of the first outlet, and the second cylinder is made of a steel pipe.

Further, the mixing unit further includes: and the gas distributor is arranged in the second cylinder and communicated with the hydrogen inlet, and the gas distributor is used for uniformly distributing hydrogen into the material.

Further, the gas distributor comprises: the body is provided with an inlet and an outlet, and the inlet of the body is communicated with the hydrogen inlet of the second cylinder; and the inorganic membrane is arranged on the outlet of the body and is provided with a plurality of through holes, preferably, the inorganic membrane is a ceramic membrane, and more preferably, the diameter of the through holes of the ceramic membrane is between 0.3 and 1.0 μm.

Further, the gas distributor further comprises: the molecular sieve is attached to the inorganic membrane, preferably, the molecular sieve is FAU type molecular sieve, and more preferably, the thickness of the FAU type molecular sieve is less than 1.0 μm.

Further, the sub-reactors further comprise: and the pump body is arranged on a pipeline between the outlet of the first cylinder and the outlet of the strengthening device and is used for conveying materials.

Further, the heavy oil hydrotreating system also includes: and a hydrogen outlet of the hydrogen supply device is communicated with a hydrogen inlet of the second cylinder, and the purity of the hydrogen provided by the hydrogen supply device is A, wherein A is more than or equal to 20%.

Further, the hydrogen supply apparatus produces hydrogen gas by cracking methane.

Further, the heavy oil hydrotreating system also includes: the rectifying tower is used for separating gas-phase products of the materials according to a boiling point range, and an inlet of the rectifying tower is communicated with a gas-phase product outlet of the first cylinder; the non-condensable gas outlet at the top of the rectifying tower is communicated with the inlet of the hydrogen supply device, or the non-condensable gas outlet at the top of the rectifying tower is communicated with the hydrogen inlet of the second cylinder.

Further, the pressure in the heavy oil hydrotreating system is less than 0.1 MPa.

Further, the reaction temperature of the material in the heavy oil hydrotreating system is between 350 ℃ and 410 ℃.

By applying the technical scheme of the invention, the mixing unit and the strengthening device are arranged in the heavy oil hydrotreating system, and the strengthening device can provide energy for the material after heavy oil and hydrogen are mixed so as to enable the material to be subjected to cracking reaction, so that the heavy oil hydrotreating system can treat the heavy oil by adopting a hydrotreating process without higher pressure and temperature and higher hydrogen consumption, and the operation cost of the heavy oil hydrotreating system can be reduced. The heavy oil hydrotreating system can operate under normal pressure and at a lower temperature, and the performance requirement on the system is reduced, so that the structure of the system can be simplified, and the investment cost of the heavy oil hydrotreating system can be reduced.

Drawings

The accompanying drawings, which are incorporated in and constitute a part of this application, illustrate embodiments of the invention and, together with the description, serve to explain the invention and not to limit the invention. In the drawings:

FIG. 1 shows a schematic diagram of a heavy oil hydroprocessing system provided by the present invention;

FIG. 2 shows a top view of the heavy oil hydroprocessing system of FIG. 1;

FIG. 3 shows a schematic of the configuration of a mixing unit in a heavy oil hydroprocessing system;

FIG. 4 shows a schematic of the structure of a plasma unit in a heavy oil hydroprocessing system;

FIG. 5 shows a schematic of the configuration of a cavitation unit in a heavy oil hydroprocessing system;

FIG. 6 shows a schematic diagram of a configuration of a stirring unit in a heavy oil hydroprocessing system;

fig. 7 shows a schematic of the structure of an impingement unit in a heavy oil hydroprocessing system.

Wherein the figures include the following reference numerals:

10. a mixing unit; 11. a second cylinder; 12. a gas distributor; 20. a plasma unit; 21. a third cylinder; 22. a dielectric; 23. an electrode; 30. a cavitation unit; 31. a cavitation plate group; 31a, a first plate body; 31b, a second plate body; 40. a stirring unit; 41. a rotating shaft; 42. a paddle; 43. an arc-shaped baffle plate; 50. a striking unit; 51. a support; 52. a delivery pipe; 60. a pump body; 100. a sub-reactor; 200. a main reactor; 210. a first cylinder.

Detailed Description

The technical solution in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. The following description of at least one exemplary embodiment is merely illustrative in nature and is in no way intended to limit the invention, its application, or uses. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

As shown in fig. 1 to 7, an embodiment of the present invention provides a heavy oil hydrotreating system including a main reactor 200 and a sub-reactor 100. Wherein, the main reactor 200 includes a first barrel 210, materials can be added into the first barrel 210 or discharged from the first barrel 210, and materials can also be reacted in the first barrel 210. The sub-reactor 100 includes a mixing unit 10 and an intensifying apparatus. Wherein the mixing unit 10 is used for mixing the material and the hydrogen. As shown in fig. 3, the mixing unit 10 includes a second cylinder 11, the second cylinder 11 is provided with a material inlet, a hydrogen inlet and a first outlet, and the material inlet is communicated with the outlet of the first cylinder 210. The inlet of the reinforcing device is communicated with the first outlet of the second cylinder 11, and the outlet of the reinforcing device is communicated with the accommodating cavity of the first cylinder 210.

The enhancement device is used for providing energy for the materials to enable the materials to generate cracking reaction. The energy provided by the strengthening device can enable hydrocarbon molecules and hydrogen molecules in the material to obtain enough external energy, under the action of the catalyst, molecular bonds of the hydrocarbon molecules, particularly polycyclic aromatic hydrocarbons, are cut off to generate hydrocarbon ions, and hydrogen bonds of the hydrogen molecules are cut off to generate hydrogen ions. The hydrocarbon ions and hydrogen ions combine to form new compounds to complete the cracking reaction. The scheme can replace the original scheme that the materials can react at high temperature and high pressure through the action of the strengthening device.

By applying the technical scheme of the invention, the strengthening device can provide energy for the material mixed by the heavy oil and the hydrogen to enable the material to generate cracking reaction, so that the heavy oil hydrotreating system can treat the heavy oil by adopting a hydrotreating process without higher pressure and temperature and higher hydrogen consumption, thereby reducing the operation cost of the heavy oil hydrotreating system. In addition, the heavy oil hydrotreating system can operate under normal pressure and at a lower temperature, and the performance requirement on the system is reduced, so that the structure of the system can be simplified, and the investment cost of the heavy oil hydrotreating system can be reduced.

Specifically, the intensifying apparatus includes an intensifying unit, which is one or more of the plasma unit 20, the cavitation unit 30, the stirring unit 40, and the striking unit 50. The plasma unit 20 is used for ionizing the materials, the cavitation unit 30 is used for generating cavitation to the materials, the stirring unit 40 is used for stirring the materials, and the impact unit 50 is used for impacting the materials entering the containing cavity of the first cylinder 210. By setting the strengthening device as the strengthening unit and selecting the type of the strengthening unit, the proper strengthening device can be set according to production requirements, so that enough energy is provided for the mixed materials, and the materials are subjected to cracking reaction. Moreover, the optional provision of the enhancement device can enhance the applicability of the heavy oil hydrotreating system. The intensifying apparatus may be provided as any one, any two, any three, or all four of the plasma unit 20, the cavitation unit 30, the stirring unit 40, and the striking unit 50. The multiple strengthening units can be connected in parallel or in series, and can also be connected in parallel or in series at the same time. When the number of types of the reinforcement units in the reinforcement device is reduced, the manufacturing cost of the device can be reduced, and when the number of types of the reinforcement units in the reinforcement device is increased, the reaction efficiency of the system can be improved. In actual production, cost and efficiency should be balanced according to different situations.

Only one type of the reinforcement unit may be included in the reinforcement device, in which case the first outlet of the second cylinder 11, the reinforcement unit and the first cylinder 210 are smoothly communicated. For example, the strengthening means includes only the striking unit 50, and the first outlet of the second cylinder 11, the striking unit 50 and the first cylinder 210 are sequentially communicated. The reinforcing means may include a plurality of reinforcing units, and when one of the reinforcing units is the striking unit 50, an outlet of the striking unit 50 is communicated with the receiving cavity of the first cylinder 210, and the first outlet of the second cylinder 11, the other reinforcing units and the striking unit 50 are sequentially communicated. I.e. when the impingement unit 50 is included in a sub-reactor, the impingement unit 50 is arranged at the rear end in the material flow direction. After being mixed in the second cylinder 11, the heavy oil and the hydrogen sequentially enter the plurality of strengthening units, and energy is sequentially provided through the action of the plurality of strengthening units, so that the materials are fully reacted.

In the present application, the intensifying apparatus may include a plurality of intensifying units, each of which is one of the plasma unit 20, the cavitation unit 30, and the agitation unit 40. In this case, the reinforcement means does not include the striking unit 50, and the first outlet of the second cylinder 11, the plurality of reinforcement units, and the receiving chamber of the first cylinder 210 are sequentially communicated. After being mixed in the second cylinder 11, the heavy oil and the hydrogen sequentially enter the plurality of strengthening units, and energy is sequentially provided through the action of the plurality of strengthening units, so that the materials are fully reacted.

As shown in fig. 4, the plasma unit 20 includes a third cylinder 21, a dielectric 22, and an electrode 23. The third cylinder 21 has a first cylinder wall and a second cylinder wall, and the first cylinder wall is disposed inside the second cylinder wall. And a first cavity is arranged between the first cylinder wall and the second cylinder wall, a second cavity is arranged in the first cylinder wall, and materials can flow in the first cavity. A dielectric 22 is disposed in the second cavity. The electrode 23 penetrates at least partially into the dielectric 22, and one end of the electrode 23 is connected to a high voltage power supply. So configured, the electrode 23 inputted with the high voltage power generates a high voltage electric field, and the high voltage electric field is discharged to form Plasma (DBD Plasma) under the barrier of the insulating dielectric 22, so that the material is dissociated into ions to cause the material to undergo a cracking reaction.

In this embodiment, the cavitation unit 30 includes a fourth cylinder in which the material may flow. The cavitation unit 30 also includes one or both of a cavitation plate set 31 and a cavitation nozzle. The cavitation nozzle may be provided as one or more of a Venturi Tube (Venturi Tube), an Organ Tube (Organ Tube) and a Helmholtz Tube (Helmholtz Tube). When the cavitation unit 30 includes the cavitation plate group 31, the cavitation plate group 31 is disposed in the fourth cylinder; when the cavitation unit 30 includes a cavitation nozzle, the cavitation nozzle is also disposed within the fourth cylinder. In the cavitation unit 30, the flowing material can generate cavitation effect under the cutting action of the cavitation plate group 31 or the cavitation nozzle. The cavitation effect can provide energy for the material, so that molecular bonds of the material are broken, and cracking reaction is carried out.

Cavitation bubbles are generated in the area where cavitation effects occur and undergo the process of formation and collapse. The collapse of the vacuole can make the temperature of the gas phase region reach about 5200K, the temperature of the liquid phase region reach about 1900K, the local pressure can reach 50.5MPa, and the temperature change rate can reach 109K/s. The collapse of the vacuole is accompanied by a strong shock wave and a microjet with a velocity of up to 110 m/s. The high energy locally generated by cavitation is sufficient to crack molecular bonds including fused ring aromatics in the material, thereby allowing the material to react sufficiently.

As shown in fig. 5, the cavitation plate group 31 includes a first plate 31a and a second plate 31b, and both the first plate 31a and the second plate 31b are fixedly disposed in the fourth cylinder. The first plate 31a is provided with a plurality of through holes, the second plate 31b is also provided with a plurality of through holes, and an included angle is formed between the second plate 31b and the first plate 31 a. The arrangement can increase the contact area of the cavitation plate group 31 and the material flowing through the fourth cylinder, and can strengthen the impact of the material on the first plate body 31a and the second plate body 31b, so that stronger cavitation effect can be generated. The cavitation effect enhancement can provide higher energy for the material, thereby accelerating the cracking reaction efficiency of the material.

Further, in this embodiment, a peripheral edge of at least a portion of the first plate body 31a may be configured as a sawtooth shape, a peripheral edge of at least a portion of the second plate body 31b may be configured as a sawtooth shape, and both a peripheral edge of at least a portion of the first plate body 31a and a peripheral edge of at least a portion of the second plate body 31b may be configured as a sawtooth shape. So set up, can further increase the area of contact of material and cavitation board group 31 through the effect of zigzag structure to further strengthen the impact of material and cavitation board group 31, thereby produce stronger cavitation effect. The cavitation effect enhancement can provide higher energy for the material, thereby accelerating the cracking reaction efficiency of the material.

In this embodiment, the cavitation plate group 31 may be provided in plurality, and the plurality of cavitation plate groups 31 are sequentially disposed in the fourth cylinder along the flow direction of the material. Therefore, after passing through one cavitation plate group 31, the unreacted materials can pass through the next cavitation plate group 31 to continue to generate cavitation effect and react. Therefore, the plurality of cavitation plate groups 31 may promote the cracking reaction of the material.

As shown in fig. 6, the stirring unit 40 includes a fifth cylinder, a rotation shaft 41, and a plurality of blades 42. Wherein the material can flow in the fifth cylinder. The rotating shaft 41 is rotatably provided in the fifth cylinder, and the axial direction of the rotating shaft 41 is arranged in the flow direction of the material. A plurality of paddles 42 are provided on the rotating shaft 41 at intervals in the circumferential direction of the rotating shaft 41. When the material flows through the fifth cylinder, the plurality of blades 42 rotate in the fifth cylinder, and the stirring of the blades 42 on the material can not only fully mix the materials with different components or different forms, but also provide energy for the material, so that the material is subjected to a cracking reaction.

Specifically, the gas-liquid-solid three-phase materials can be fully mixed and contacted through the stirring action of the blades 42, and the hydrogen and the heavy oil can be fully mixed and contacted, so that the material transfer is enhanced. Moreover, the material can be cavitated by the stirring action of the blades 42. Specifically, when the blades 42 rotate, the material behind the blades 42 is reduced, the pressure behind the blades 42 is reduced, and the tiny light hydrocarbon bubbles or hydrogen bubbles in the material are increased in a low-pressure state, so as to form a cavitation flow (cavitation flow) region. At the instant when the next paddle 42 moves into the cavitation flow region, the paddle 42 compresses the cavitation bubbles, causing them to collapse. When the vacuoles are broken, high temperature and high pressure are generated, and the high temperature and high pressure enable the materials to generate cracking reaction.

Further, the stirring unit 40 further includes a plurality of arc baffles 43, the plurality of arc baffles 43 are fixedly disposed between the fifth cylinder and the plurality of paddles 42, and the plurality of arc baffles 43 are disposed at intervals along the circumferential direction of the rotating shaft 41. When stirring the material, a plurality of paddles 42 can drive the material to move from the rotating shaft 41 to the inner wall of the fifth cylinder, and due to the blocking effect of the arc-shaped baffles 43, the material can be concentrated through the gaps between the paddles 42 and the arc-shaped baffles 43 and the gaps between the adjacent arc-shaped baffles 43. When passing through the gap, the paddles 42 or the curved baffles 43 produce a shearing action on the material that helps crack, ring open, and react the macromolecules in the heavy oil. Therefore, the reaction efficiency of the materials can be enhanced by providing the arc-shaped baffle 43.

As shown in fig. 1 and 7, the striking unit 50 is disposed at an upper portion of the receiving chamber of the first cylinder 210. The striking unit 50 includes a bracket 51 and a delivery pipe 52. Wherein, the bracket 51 is fixed on the inner side wall of the first cylinder 210; the delivery tube 52 is fixed on the bracket 51, and the bracket 51 can support the delivery tube 52. And the inlet of the conveying pipe 52 is communicated with the first outlet of the second cylinder 11, and the material directly output from the second cylinder 11 or the material which is output from the second cylinder 11 and then passes through other strengthening units enters the accommodating cavity of the first cylinder 210 through the conveying pipe 52. The material enters the accommodating cavity from the conveying pipe 52 at a certain speed, and when the material enters the accommodating cavity, the material collides with the material or the material collides with the inner side wall of the first cylinder 210. The kinetic energy of the material at the moment of impact is converted into potential energy and heat energy of the liquid molecular layer, so that the material obtains high energy capable of breaking molecular bonds, and the molecular bonds of the material are broken to further generate cracking reaction. The reaction of the materials can be promoted by the action of the striking unit 50, thereby enhancing the treatment and recovery of the heavy oil.

Moreover, the impact unit 50 is disposed at the upper portion of the heavy oil in the accommodating chamber of the first cylinder 210, so that in the process of material impact, the flash evaporation of the material can be accelerated, the product after the material reaction can be gasified, the separation and recovery of the product are facilitated, and the treatment effect on the heavy oil is improved.

In the present embodiment, the reinforcing means of the sub-reactor 100 includes the striking unit 50, an inlet of the striking unit 50 is communicated with the first outlet of the second barrel 11, and an outlet of the striking unit 50 is communicated with the receiving chamber of the first barrel 210. The number of the sub-reactors 100 is at least two, and the outlets of the impingement units 50 of at least two sub-reactors 100 are spaced apart. So configured, the materials entering the first barrel 210 from different striking units 50 can be caused to strike each other. The materials in the different striking units 50 have a certain speed, and they strike each other to intensify the striking process, so that the kinetic energy of the materials is more converted into potential energy and heat energy to promote the reaction of the materials.

Specifically, as shown in fig. 7, the materials in the impact unit 50 are conveyed through the conveying pipes 52, the outlets of the two conveying pipes 52 are arranged oppositely, so that the materials in the two conveying pipes 52 flow in opposite directions, and the materials are impacted oppositely after flowing out of the outlets, so that the kinetic energy of the materials is further converted into potential energy and thermal energy to promote the reaction of the materials. Alternatively, the brackets 51 in different percussion units 50 may be interconnected to increase the structural strength of the device and improve the service life of the percussion unit 50. In order to ensure the impact effect, the flow rate of the material in the conveying pipe 52 may be set to 20-50m/s in this embodiment.

As shown in fig. 3, the cross-sectional area of the inner wall of the second cylinder 11 is larger than that of the inner wall of the first outlet, so that a higher pressure can be maintained when the heavy oil and the hydrogen gas are introduced into the containing cavity of the second cylinder 11, thereby facilitating the mixing of the heavy oil and the hydrogen gas and promoting the reaction of the heavy oil and the hydrogen gas. Because the heavy oil hydrotreating system is provided with the strengthening device, the system can operate under lower pressure and temperature, and the performance requirement on the second cylinder 11 is reduced, so that the structure of the second cylinder 11 can be simplified, and the investment cost of the heavy oil hydrotreating system can be reduced. Specifically, the second cylinder 11 may be made of a steel pipe, which can significantly reduce the investment cost of the heavy oil hydrotreating system compared to using a special pressure vessel.

In this embodiment, the mixing unit 10 further includes a gas distributor 12, the gas distributor 12 being disposed in the second cylinder 11, the gas distributor 12 being in communication with the hydrogen inlet, the gas distributor 12 being for uniformly distributing hydrogen into the heavy oil. Through setting up gas distributor 12, can disperse the different positions in the second barrel 11 with the hydrogen that concentrates to get into in the second barrel 11 to increase the area of contact of hydrogen and heavy oil, thereby make hydrogen and heavy oil homogeneous mixing, be favorable to subsequent reaction like this.

For better gas distribution, a permeable membrane may be provided in the gas distributor 12. Meanwhile, in order to adapt to the working environment with high temperature and large disturbance of liquid phase, the permeable membrane can be set to be an inorganic membrane. The inorganic film has the advantages of high strength, good thermal stability, corrosion resistance, easy cleaning and the like, so the inorganic film can meet the use requirement.

Specifically, the gas distributor 12 includes a body and an inorganic membrane. Wherein the body has an inlet and an outlet which are communicated with each other, and the inlet of the body is communicated with the hydrogen inlet of the second cylinder 11. The inorganic membrane is disposed on the outlet of the body, and the inorganic membrane has a plurality of through holes. So set up, hydrogen passes through a plurality of through-holes on the inorganic membrane after getting into the body and disperses from different positions and gets into in the second barrel 11 to with the heavy oil homogeneous mixing of different positions.

In the heavy oil hydrotreating system, the cracking reaction can be carried out without using hydrogen with higher purity, so that the gas with less hydrogen content can be used as a hydrogen source to reduce the operation cost of the system. For example, the gas obtained by cracking methane may be used as a hydrogen source, or a hydrogen-containing gas obtained by another method may be used. The gas containing less hydrogen will contain other gases, e.g. CO, CO₂、CH₄Or liquefied gas such as carbon 2 and carbon 3 or water vapor. Some of the gas molecules have large size, so when the inorganic membrane is selected, the inorganic membrane with large through hole size and no filterability is adopted to ensure that the gas can smoothly pass through.

In the present embodiment, the inorganic membrane may be provided as a ceramic membrane. The ceramic membrane should have the characteristics of high strength, good thermal stability, single pore size distribution and small flux attenuation. For example, Al may be selected as a metal oxide ceramic material₂O₃Or ZrO₂A ceramic membrane which is a framework. Preferably, the diameter of the through-holes of the ceramic membrane in this embodiment is set to be between 0.3 μm and 1.0 μm, so that deionized water having a relatively large molecular size can pass through the through-holes. The ceramic membrane, which is capable of passing deionized water, may also optionally allow the gas to pass through and exhibit a small gas resistance to allow the gas to pass through the ceramic membrane smoothly and mix with the heavy oil.

Optionally, gas distributor 12 further comprises a molecular sieve attached to the inorganic membrane. By arranging the molecular sieve, the pore size of the inorganic membrane can be properly restricted, which is helpful for stabilizing the gas pressure entering the liquid phase on one hand, and enables hydrogen and other gases to rapidly enter the liquid phase at a certain acceleration and more tiny bubbles on the other hand. Preferably, FAU-type molecular sieves having a thickness of less than 1.0 μm may be attached to the ceramic membrane.

The gas distributor 12 has dual functions by providing an inorganic membrane and a molecular sieve: on one hand, hydrogen can enter heavy oil in the form of tiny bubbles and is parallel or combined with cavitation bubbles generated by the heavy oil in longitudinal wave oscillation, so that the hydrogen is filled in the cavitation bubbles or nearby the cavitation bubbles, and the hydrocracking process is finished at the moment when the cavitation bubbles collapse; on the other hand, the silica-alumina ratio of the molecular sieve in contact with the heavy oil on the surface layer of the inorganic membrane can be adjusted, so that the gas distributor 12 can play a role in catalyzing the cracking reaction. The arrangement is beneficial to the uniform mixing of the hydrogen and the heavy oil and the cracking reaction of the hydrogen and the heavy oil.

In this embodiment, the sub-reactor 100 further comprises a pump 60, the pump 60 is disposed on the pipeline between the outlet of the first cylinder 210 and the outlet of the intensification device, and the pump 60 is used for conveying materials. The pump body 60 is provided to ensure the flow of the materials inside the sub-reactors 100 and between the sub-reactors 100 and the main reactor 200. As shown in fig. 1, the pump 60 may be provided between the first cylinder 210 and the mixing unit 10, the pump 60 may be provided between the mixing unit 10 and the intensifying apparatus, or the pump 60 may be provided inside the intensifying apparatus. The pump body 60 may be provided in plurality according to production needs.

By providing the pump body 60, the materials in the sub-reactors 100 and the main reactor 200 can be circulated to fully react the materials in the system. After the materials pass through the sub-reactors 100, the reacted products may be separated in the first barrel 210, the unreacted materials flow into the bottom of the first barrel 210, and then the pump 60 may transport the materials at the bottom of the first barrel 210 to the sub-reactors 100 again for further reaction. Thus, the heavy oil can be fully reacted, and the treatment efficiency and the utilization rate of the heavy oil are improved. In this embodiment, the residence time of the heavy oil as a material in the heavy oil hydroprocessing system is between 30 minutes and 90 minutes, and the average is 60 minutes, so as to achieve the balance of the treatment efficiency and the utilization rate, thereby maximizing the economic benefit. Of course, the residence time of the material can be set to other values according to the needs of the process.

Under the condition of unchanged process, the conversion rate of the product is closely related to the quality of the heavy oil. For example, for heavy oil of heavy crude oil, the technical scheme of the embodiment has better economic index when the utilization rate of the end point of 500 ℃ is 70-90%.

Further, the heavy oil hydrotreating system also includes a hydrogen supply device, a hydrogen outlet of the hydrogen supply device is communicated with a hydrogen inlet of the second cylinder 11, and the hydrogen supply device is used for supplying hydrogen to the mixing unit 10. In the heavy oil hydrotreating system, the cracking reaction can be carried out without using hydrogen with higher purity, so that the gas with less hydrogen content can be used as a hydrogen source to reduce the operation cost of the system. The purity of the hydrogen provided by the hydrogen supply device is more than or equal to 20 percent, so that the reaction requirement of the heavy oil can be met. The use of a gas containing a small amount of hydrogen as a hydrogen source can reduce the cost of raw materials for producing hydrogen, and therefore can significantly reduce the operating cost of the system.

The hydrogen consumption of the prior heavy oil hydrotreating system is 150NM³/M³To 300NM³/M³While the hydrogen consumption of the heavy oil hydrotreating system of the embodiment is less than or equal to 50NM³/M³The heavy oil hydrotreating system can be operated, so that the hydrogen consumption can be remarkably reduced, and the operation cost of the system can be reduced.

Specifically, the hydrogen supply device can prepare hydrogen by methane cracking, so that the purity requirement of the system on the hydrogen can be met, and the cost of raw materials can be reduced. The gas produced after methane cracking contains other gases, and the gases can be sent to the mixing unit 10 together without being separated by using the system.

In this embodiment, the heavy oil hydrotreating system further includes a rectifying tower for separating the gas-phase products of the material by boiling point range. The inlet of the rectifying tower is communicated with the gas-phase product outlet of the first cylinder 210, and the non-condensable gas outlet at the top of the rectifying tower is communicated with the inlet of the hydrogen supply device. Or the inlet of the rectifying tower is communicated with the gas-phase product outlet of the first cylinder 210, and the non-condensable gas outlet at the top of the rectifying tower is communicated with the hydrogen inlet of the second cylinder 11. The device can separate gas-phase products of materials according to boiling point range by the rectifying tower, thereby converting heavy oil into utilizable products.

In order to improve the utilization rate of the hydrogen, the unreacted hydrogen can be recovered. In the existing heavy oil hydrotreating system, the recovered hydrogen needs to be eluted with impurities through a solvent or an alkali solution, or can be reused through solid adsorption. The system of this embodiment is more easily operated in a lower pressure and temperature environment, so hydrogen gas escapes from the liquid phase. Moreover, because the system has low requirements for the purity of the hydrogen, the recovered hydrogen can be reused without treatment. Therefore, the technical scheme of the embodiment can reduce the recovery cost of the hydrogen.

Since the non-condensable gas at the top of the rectifying tower contains a large amount of unreacted hydrogen, the non-condensable gas containing hydrogen can be recovered and reused in a low-cost manner by the arrangement. Specifically, the non-condensable gas may be supplied to the hydrogen supply device, and the non-condensable gas may be mixed with hydrogen gas generated in the hydrogen supply device and then supplied to the mixing unit 10. Or the non-condensable gas is directly conveyed to the mixing unit 10 for recycling.

The pressure of the prior heavy oil hydrotreating system during operation is between 5.0MPa and 24.13 MPa. In the embodiment, the pressure in the heavy oil hydrotreating system is less than 0.1MPa, that is, the system can operate under normal pressure. Compared with the existing heavy oil hydrotreating system, the operation pressure of the system is greatly reduced, so that the performance requirement on the system can be reduced on one hand, and the investment cost of the system can be reduced, and the operation parameter requirement on the system can be reduced on the other hand, and the operation cost of the system can be reduced.

The reaction temperature of the prior heavy oil hydrotreating system during operation is between 370 ℃ and 460 ℃. In this application, the reaction temperature of the feedstock in the heavy oil hydroprocessing system is between 350 ℃ and 410 ℃. This is significantly lower than the reaction temperature of the existing heavy oil hydroprocessing system, and therefore, the energy consumption of the system can be reduced, thereby reducing the operation cost of the system.

From the above, compared with the prior art, the heavy oil hydrotreating system provided by the invention can be operated under the environment with normal pressure and lower temperature, and has low requirement on the purity of hydrogen and low consumption of hydrogen. Due to the characteristics, the technical scheme of the invention can reduce the investment cost and the operation cost of the heavy oil hydrotreating system. Through calculation, the investment cost of the heavy oil hydrotreating system provided by the invention is only 1/10-1/20 of the investment cost of the existing system, and the operation cost is only 1/2-1/3 of the operation cost of the existing system, so that the technical scheme of the invention can obtain remarkable economic benefit.

The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments according to the present application. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.

The relative arrangement of the components and steps, the numerical expressions and numerical values set forth in these embodiments do not limit the scope of the present invention unless specifically stated otherwise. Meanwhile, it should be understood that the sizes of the respective portions shown in the drawings are not drawn in an actual proportional relationship for the convenience of description. Techniques, methods, and apparatus known to those of ordinary skill in the relevant art may not be discussed in detail but are intended to be part of the specification where appropriate. In all examples shown and discussed herein, any particular value should be construed as merely illustrative, and not limiting. Thus, other examples of the exemplary embodiments may have different values. It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, further discussion thereof is not required in subsequent figures.

In the description of the present invention, it is to be understood that the orientation or positional relationship indicated by the orientation words such as "front, rear, upper, lower, left, right", "lateral, vertical, horizontal" and "top, bottom", etc. are usually based on the orientation or positional relationship shown in the drawings, and are only for convenience of description and simplicity of description, and in the case of not making a reverse description, these orientation words do not indicate and imply that the device or element being referred to must have a specific orientation or be constructed and operated in a specific orientation, and therefore, should not be considered as limiting the scope of the present invention; the terms "inner and outer" refer to the inner and outer relative to the profile of the respective component itself.

Spatially relative terms, such as "above … …," "above … …," "above … …," "above," and the like, may be used herein for ease of description to describe one device or feature's spatial relationship to another device or feature as illustrated in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations of the device in use or operation in addition to the orientation depicted in the figures. For example, if a device in the figures is turned over, devices described as "above" or "on" other devices or configurations would then be oriented "below" or "under" the other devices or configurations. Thus, the exemplary term "above … …" can include both an orientation of "above … …" and "below … …". The device may be otherwise variously oriented (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein interpreted accordingly.

It should be noted that the terms "first", "second", and the like are used to define the components, and are only used for convenience of distinguishing the corresponding components, and the terms have no special meanings unless otherwise stated, and therefore, the scope of the present invention should not be construed as being limited.

Claims

1. A heavy oil hydroprocessing system, characterized by comprising a main reactor (200) and at least one sub-reactor (100), the main reactor (200) comprising a first barrel (210), the sub-reactor (100) comprising:

the mixing unit (10) is used for mixing materials and hydrogen, the mixing unit (10) comprises a second cylinder (11), a material inlet, a hydrogen inlet and a first outlet are formed in the second cylinder (11), and the material inlet is communicated with the outlet of the first cylinder (210);

an inlet of the strengthening device is communicated with the first outlet of the second cylinder (11), an outlet of the strengthening device is communicated with the accommodating cavity of the first cylinder (210), and the strengthening device is used for providing energy for materials to enable the materials to generate cracking reaction;

the strengthening device comprises a strengthening unit, the strengthening unit is a plurality of plasma unit (20), a cavitation unit (30), a stirring unit (40) and an impact unit (50), the plasma unit (20) is used for ionizing materials, the cavitation unit (30) is used for enabling the materials to generate cavitation, the stirring unit (40) is used for stirring the materials, and the impact unit (50) is used for impacting the materials entering a containing cavity of the first cylinder (210);

the striking unit (50) is disposed at an upper portion of a receiving chamber of the first cylinder (210), the striking unit (50) including: the bracket (51) is fixed on the inner side wall of the first cylinder (210); the conveying pipe (52) is fixed on the bracket (51), and the inlet of the conveying pipe (52) is communicated with the first outlet of the second cylinder (11);

the cavitation unit (30) comprises: a fourth cylinder; a cavitation plate group (31) disposed within the fourth cylinder; and/or a cavitation nozzle disposed within the fourth barrel.

2. The heavy oil hydroprocessing system according to claim 1, wherein the outlet of the impingement unit (50) communicates with the receiving cavity of the first cylinder (210), and the first outlet of the second cylinder (11), the other enhancement units and the impingement unit (50) communicate in sequence.

3. The heavy oil hydroprocessing system of claim 1, wherein the plasma unit (20) comprises:

the third barrel (21) is provided with a first barrel wall and a second barrel wall, the first barrel wall is arranged on the inner side of the second barrel wall, a first cavity is arranged between the first barrel wall and the second barrel wall, a second cavity is arranged in the first barrel wall, and materials can flow in the first cavity;

a dielectric (22) disposed in the second cavity;

an electrode (23) at least partially penetrating into the dielectric (22), one end of the electrode (23) being connected to a high voltage power supply.

4. The heavy oil hydroprocessing system of claim 1, wherein the cavitation unit (30) comprises a cavitation plate group (31), the cavitation plate group (31) comprising:

the first plate body (31 a), wherein a plurality of through holes are formed in the first plate body (31 a);

the second plate body (31 b), be provided with a plurality of through-holes on the second plate body (31 b), the second plate body (31 b) with the contained angle has between first plate body (31 a).

5. The heavy oil hydroprocessing system of claim 4, wherein at least a portion of the first plate body (31 a) has a serrated perimeter and/or at least a portion of the second plate body (31 b) has a serrated perimeter.

6. The heavy oil hydroprocessing system of claim 1, wherein the cavitation plate group (31) is plural, and a plurality of the cavitation plate groups (31) are sequentially disposed in the fourth cylinder in a flow direction of the material.

7. The heavy oil hydroprocessing system of claim 1, wherein the agitation unit (40) comprises:

a fifth cylinder;

the rotating shaft (41) is rotatably arranged in the fifth cylinder, and the axial direction of the rotating shaft (41) is arranged along the flowing direction of the materials;

a plurality of paddles (42), a plurality of paddles (42) are arranged on the rotating shaft (41) at intervals along the circumferential direction of the rotating shaft (41).

8. The heavy oil hydroprocessing system of claim 7, wherein the agitation unit (40) further comprises:

and the arc-shaped baffles (43) are fixedly arranged between the fifth cylinder and the paddles (42), and the arc-shaped baffles (43) are arranged at intervals along the circumferential direction of the rotating shaft (41).

9. The heavy oil hydroprocessing system according to claim 1, wherein the impact unit (50) is disposed at an upper portion of the receiving chamber of the first cylinder (210), the impact unit (50) comprising:

the bracket (51) is fixed on the inner side wall of the first cylinder (210);

and the conveying pipe (52) is fixed on the bracket (51), and the inlet of the conveying pipe (52) is communicated with the first outlet of the second cylinder (11).

10. The heavy oil hydroprocessing system of claim 1,

the strengthening device of the sub-reactor (100) comprises the impact unit (50), the inlet of the impact unit (50) is communicated with the first outlet of the second cylinder (11), and the outlet of the impact unit (50) is communicated with the accommodating cavity of the first cylinder (210);

the number of the sub-reactors (100) is at least two, outlets of the impact units (50) of at least two sub-reactors (100) are arranged at intervals, and materials entering the first cylinder (210) from different impact units (50) are impacted.

11. The heavy oil hydroprocessing system according to claim 1, wherein the cross-sectional area of the inner wall of the second cylinder (11) is larger than the cross-sectional area of the inner wall of the first outlet, and the second cylinder (11) is made of a steel pipe.

12. The heavy oil hydroprocessing system according to claim 1, wherein the mixing unit (10) further comprises:

the gas distributor (12) is arranged in the second cylinder (11), the gas distributor (12) is communicated with the hydrogen inlet, and the gas distributor (12) is used for uniformly distributing hydrogen into the material.

13. The heavy oil hydroprocessing system according to claim 12, wherein the gas distributor (12) comprises:

a body having an inlet and an outlet, the inlet of the body communicating with the hydrogen inlet of the second cylinder (11);

an inorganic membrane disposed on the outlet of the body, the inorganic membrane having a plurality of through holes.

14. The heavy oil hydroprocessing system of claim 13, wherein the inorganic membrane is a ceramic membrane.

15. The heavy oil hydroprocessing system of claim 14, wherein the through-holes of the ceramic membrane have a diameter between 0.3 μ ι η and 1.0 μ ι η.

16. The heavy oil hydroprocessing system according to claim 13, wherein the gas distributor (12) further comprises:

a molecular sieve attached to the inorganic membrane.

17. The heavy oil hydroprocessing system of claim 16, wherein the molecular sieve is a FAU-type molecular sieve.

18. The heavy oil hydroprocessing system of claim 17, wherein the FAU-type molecular sieve has a thickness of less than 1.0 μ ι η.

19. The heavy oil hydroprocessing system of claim 1, wherein the sub-reactor (100) further comprises:

the pump body (60) is arranged on a pipeline between the outlet of the first cylinder (210) and the outlet of the strengthening device, and the pump body (60) is used for conveying materials.

20. The heavy oil hydroprocessing system of claim 1, further comprising:

and a hydrogen outlet of the hydrogen supply device is communicated with a hydrogen inlet of the second cylinder (11), and the purity of the hydrogen provided by the hydrogen supply device is A, wherein A is more than or equal to 20%.

21. The heavy oil hydroprocessing system of claim 20, wherein the hydrogen supply unit produces hydrogen gas from methane cracking.

22. The heavy oil hydroprocessing system of claim 20, further comprising:

the rectifying tower is used for separating gas-phase products of the materials according to a boiling point range, and an inlet of the rectifying tower is communicated with a gas-phase product outlet of the first cylinder (210);

and a non-condensable gas outlet at the top of the rectifying tower is communicated with an inlet of the hydrogen supply device, or the non-condensable gas outlet at the top of the rectifying tower is communicated with a hydrogen inlet of the second cylinder (11).

23. The heavy oil hydroprocessing system of claim 1, wherein the pressure within the heavy oil hydroprocessing system is less than 0.1 MPa.

24. The heavy oil hydroprocessing system of claim 1, wherein the reaction temperature of the material within the heavy oil hydroprocessing system is between 350 ℃ and 410 ℃.