Slurry bed reactor and device and method for treating inferior heavy oil by coupling slurry bed reactor with catalytic cracking system

Abstract

The invention provides a slurry bed reactor and a device and method for treating inferior heavy oil by coupling the slurry bed reactor with a catalytic cracking system, the slurry bed reactor comprises a shell, a material outlet, a material inlet, a hydrogen injection port and an internal component; wherein the material outlet is formed in the top of the shell, the material inlet is formed in the bottom of the shell, the hydrogen injection port is formed in the surface of the shell, and the inner component is arranged in the shell; the inner component is provided with a material diffuser, a material distributor, an N-stage hydrogen supplementing ring pipe and a material collector from bottom to top in the axial direction of the shell; n > = 1. According to the slurry bed reactor provided by the invention, the purpose of inhibiting excessive cracking of light components caused by reaction green coke deposition and material backmixing is achieved by arranging the internal component which is simple in structure and low in manufacturing cost.

Description

TECHNICAL FIELD

[0001] The present application relates to the field of heavy oil processing, and in particular to a slurry bed reactor, a device and a method for processing poor heavy oil by coupling a slurry bed reactor with a catalytic cracking system. BACKGROUND

[0002] The development of core equipment such as reactors is one of the main technical difficulties that need to be broken through in the field of processing of inferior oil. The slurry bed hydrocracking equipment is a core equipment with significant advantages in the field of processing of inferior oil. At present, the slurry bed hydrocracking equipment is mainly divided into two categories: one is the empty barrel form without internal components or with simple internal components. This type of equipment needs to be connected in series with multiple reactors or uses a single reactor connected in series with an external circulation equipment. At the same time, a high-activity oil-soluble catalyst and a complex control system are used to realize the cyclic conversion and deep cracking of inferior heavy oil. For example, patent CN201911417674.0 discloses a combined process of "solvent deasphalting + ebullated bed hydrocracking + slurry bed hydrocracking + pretreatment + catalytic cracking". The inferior heavy oil raw material is processed to obtain dry gas, liquefied gas, catalytic gasoline, catalytic diesel and catalytic heavy oil. This invention can realize the lightening of heavy oil, maximize the production of low-carbon olefins, and prolong the operation cycle of the device. However, the slurry bed reactor of the above invention does not explicitly state whether it is an empty barrel structure or contains internal components. Moreover, the use of reactors, core equipment and fractionation equipment is relatively high, which requires a high degree of coupling of each equipment. This leads to a long and complex process, increases the potential risk of operation of the device, and inevitably increases the energy consumption and operating cost of the device. Therefore, this technology does not have economic advantages. Patent CN201810889774.2 discloses a combined process of "slurry bed + fixed bed". The inferior heavy oil raw material is treated by the slurry bed reactor, then separated into light and heavy components by the fractionation equipment, and then enters the fixed bed reactor for hydrofining. After fractionation, naphtha, kerosene, diesel and wax oil fractions are obtained. The tail oil of the slurry bed and part of the wax oil produced by the fixed bed are recycled to the slurry bed unit to continue participating in the cracking reaction. However, the internal structure of the slurry bed reactor of this invention is also not explicitly stated. Therefore, the conversion depth of the heavy oil raw material is not clear. Moreover, the invention does not set up a dedicated hydrogenation equipment and solid particle filtration equipment. If the slurry bed produces coke particles during long-term operation of the device, it will block the fixed bed unit and affect the stable operation of the device. The other type is the slurry bed reactor with complex internal components. This type of equipment can achieve the goals of strengthening the in-reactor backmixing of the reaction stream and inhibiting the deposition of coke, strengthening heat and mass transfer, and separating light components from the system while cracking heavy oil. For example, patent CN201710102972.5 discloses a slurry bed reactor. At least one heat exchange plate with a cavity and a flat structure is arranged in the slurry bed reactor. The heat exchange plate has a cooling medium inlet and a cooling medium outlet connected to the cavity. Therefore, the slurry in the slurry bed reactor can exchange heat with the cooling medium through the wall of the heat exchange plate, ensuring the stability of the temperature of the entire slurry bed reactor. However, the above internal components have problems such as complex design and operation, and high manufacturing and maintenance difficulty. Patent CN202010845269.5 discloses a combined process of "fixed bed residual oil hydrocracking + catalytic cracking + filtration unit" for processing inferior residual oil.The solid particles in the catalytic oil slurry and / or catalytic heavy cycle oil are effectively removed by using a dedicated filter unit, and then injected into a fixed bed residual oil hydrogenation unit for cyclic conversion, but the filter unit of the above process is complex in design, difficult to manufacture and install, and requires special flexible filter materials, which has a high procurement cost.

[0003] In addition, energy saving and emission reduction, and transformation and upgrading of oil refining to chemical industry are the common pursuit of people in the industry, however, the current device or system cannot realize deep conversion of inferior oil while co-producing market-needed chemical raw materials and light automotive fuel oil under the condition of maintaining stable operation of the device.

[0004] Application content

[0005] The slurry bed reactor provided by the application achieves the purpose of inhibiting over-cracking of light components caused by deposition of reaction coke and material backmixing by setting an internal component which is simple in structure and low in manufacturing cost.

[0006] The application further provides a device for processing inferior heavy oil by coupling a slurry bed reactor with a catalytic cracking system, which can realize deep conversion of inferior heavy oil, effectively inhibit the deposition risk of reaction coke, and co-produce market-needed chemical raw materials and light automotive fuel oil.

[0007] The application further provides a method for processing inferior heavy oil by using the device for processing inferior heavy oil by coupling a slurry bed reactor with a catalytic cracking system. The method can realize deep conversion of inferior oil while co-producing market-needed chemical raw materials and light automotive fuel oil under the condition of maintaining stable operation of the device.

[0008] In a first aspect, the application provides a slurry bed reactor, comprising: a shell, a material outlet, a material inlet, a hydrogen injection inlet, and an internal component; wherein the material outlet is arranged at the top of the shell, the material inlet is arranged at the bottom of the shell, the hydrogen injection inlet is arranged on the surface of the shell, and the internal component is arranged in the shell.

[0009] The internal component is provided with a material diffuser, a material distributor, N-stage hydrogen supplement ring pipes, and a material collector from bottom to top along the axial direction of the shell; N is greater than or equal to 1, the diameter of the hydrogen supplement ring pipe is smaller than the inner diameter of the shell, the pipe wall of the hydrogen supplement ring pipe is provided with at least one hydrogen inlet and a plurality of hydrogen outlets, the opening direction of the hydrogen outlet is upward along the axial direction of the shell, the hydrogen inlet corresponds to and communicates with the hydrogen injection inlet one by one, and the material collector communicates with the material outlet.

[0010] Further, the N-stage hydrogen supplement ring pipes comprise a first-stage hydrogen supplement ring pipe, a second-stage hydrogen supplement ring pipe, and a third-stage hydrogen supplement ring pipe which are spaced apart from bottom to top along the axial direction of the shell.

[0011] And / or, the diameter of the first hydrogen supplement ring pipe, the second hydrogen supplement ring pipe and the third hydrogen supplement ring pipe increases gradually.

[0012] And / or, the number of hydrogen gas outlets of the first hydrogen supplement ring pipe, the second hydrogen supplement ring pipe and the third hydrogen supplement ring pipe increases gradually.

[0013] Further, the hydrogen gas outlets are arranged equidistantly along the wall of the hydrogen supplement ring pipe, and the plane where the hydrogen gas outlets are located forms an angle of 20°-60° with the axis of the shell.

[0014] Further, the material diffuser is composed of a material bucket and a material distribution disc, and a plurality of circular holes are equidistantly arranged on the surface of the material distribution disc, and the inlet of the material bucket is communicated with or corresponds to the material inlet.

[0015] Further, the N-stage hydrogen supplement ring pipe and the material collector further comprise a foam remover and a filter filler layer, and the filter filler layer is used to retain the material with a particle size greater than 100 μm in the filter filler layer.

[0016] In the second aspect, the application provides a device for processing poor heavy oil by using a slurry bed reactor coupled catalytic cracking system, which comprises: a solid-liquid static mixer, a raw material tank, a feed pump, a heat exchanger, a hydrogen mixer, a heating furnace, the slurry bed reactor of the first aspect, a first filter, a high-pressure separator, a pressure reducing valve, a second filter, a fractionating furnace, a fractionating tower, a liquid material mixer and a riser catalytic cracking reactor which are sequentially communicated through first conveying pipelines.

[0017] The riser catalytic cracking reactor is communicated with the solid-liquid static mixer through a second pipeline, the hydrogen mixer is communicated with a hydrogen circulation compressor through a third pipeline, the high-pressure separator is communicated with the heat exchanger through a fourth pipeline, the heat exchanger is communicated with a hydrogen compressor buffer tank through a fifth pipeline, the hydrogen compressor buffer tank is communicated with the hydrogen circulation compressor through a sixth pipeline, and the hydrogen circulation compressor is communicated with the hydrogen injection inlet of the slurry bed reactor through a seventh pipeline.

[0018] In the third aspect, the application provides a method for processing poor heavy oil by using the device, which comprises the following steps:

[0019] 1) The balancing agent, the catalyst and the poor heavy oil to be processed are mixed in the solid-liquid static mixer to obtain a mixed material, and the mixed material is input into the raw material tank and pumped into the heat exchanger after being stabilized for a certain time.

[0020] 2) The mixed material after heat exchange is input into the hydrogen mixer, hydrogen output by the hydrogen circulation compressor is mixed with the mixed material in the hydrogen mixer, and then input into the heating furnace for heating, and then input into the slurry bed reactor for poor heavy oil conversion reaction to obtain a hydrocracking product.

[0021] 3) the hydrocracking product is input into a high-pressure separator after removing reaction coke particles with particle size > 50 μm through a first filter group to complete gas-liquid separation, wherein the gas phase product is input into a hydrogen compressor buffer tank after heat exchange through a heat exchanger, and then into a hydrogen circulation compressor, and the liquid phase product is input into a second filter group to remove remaining reaction coke particles with particle size > 50 μm again, and then into a fractionating furnace to be heated, and then into a fractionating tower to be fractionated to obtain gasoline, diesel, light wax oil and hydrocracking tail oil with initial boiling point of 450-500℃;

[0022] 4) the hydrocracking tail oil is mixed with the to-be-catalytically-cracked oil slurry in a liquid material mixer, and then input into a riser catalytic cracker to be catalytically cracked to obtain dry gas, liquefied gas, gasoline, diesel, catalytically-cracked oil slurry, and discharged equilibrium agent and catalyst;

[0023] 5) the catalytically-cracked oil slurry, the discharged equilibrium agent and the catalyst are input into a solid-liquid static mixer to be recycled in steps 1)-4).

[0024] Further, the operation parameters of the slurry bed reactor are as follows: the reaction temperature is 390-405℃, the reaction pressure is 12.0-14.0 MPa, the volume space velocity is 0.5-1.0 h-1, and the hydrogen / oil volume ratio is 500-800.

[0025] Further, in step 1), the mass ratio of the equilibrium agent to the catalyst is 70-80:20-30.

[0026] Further, when N≥2, the hydrogen supplement amount of the first-stage hydrogen supplement loop is 1-5% of the hydrogen feed amount of the hydrogen mixer, and the hydrogen supplement amount of the N-stage hydrogen supplement loop is 1.1-1.5 times of the hydrogen supplement amount of the N-1-stage hydrogen supplement loop.

[0027] The slurry bed reactor provided by the application can inhibit the deposition of reaction coke and the over-cracking of light components caused by material backmixing by setting the simple structure and low-cost internal components, specifically: the material diffuser and the material distributor arranged in the shell of the slurry bed reactor can optimize the material flow form in the slurry bed reactor to make the reaction materials fully mixed; the multi-stage hydrogen supplement loop arranged inside can supplement the reaction hydrogen consumption in time and improve the reaction flow, thereby effectively inhibiting the deposition of reaction coke to block the reaction equipment and the over-cracking of light components caused by reaction material backmixing; and the material collector can concentrate the materials to be output from the material outlet, thereby avoiding the gravity backfall of the materials.

[0028] The present invention provides an apparatus and method for treating inferior heavy oil using a slurry bed reactor coupled with a catalytic cracking system. This apparatus employs a coupled process concept of "staged reaction + circulating reaction + unified catalytic system," achieving continuous and stable operation of the processing unit while ensuring a high conversion rate of inferior oil. This results in the deep conversion of inferior oil and the production of more chemical feedstocks and light automotive fuel oil. Specifically, the slurry bed reactor and the riser catalytic cracker of this invention use the same catalyst. The balance agent and spent catalyst discharged from the riser catalytic cracker can be used in the slurry bed reactor system, which is beneficial for maximizing the cracking activity of the catalytic cracking catalyst and increasing the cracking depth of the inferior heavy oil. Furthermore, the coke produced in the slurry bed reactor is removed by burning off the coke along with its hydrotreating tail oil in the regenerator of the riser catalytic cracker. Attached Figure Description

[0029] The accompanying drawings, which are incorporated in and form part of this specification, illustrate embodiments consistent with the invention and, together with the description, serve to explain the principles of the invention.

[0030] Figure 1 This is a schematic diagram of a slurry bed reactor according to a specific embodiment of the present invention. In the figure, 001-material inlet, 002-material outlet, 003-material diffuser, 0031-material distribution bucket, 0032-material distribution tray, 004-material distributor, 005-N-stage hydrogen replenishment loop, 0051-first-stage hydrogen replenishment loop, 0052-second-stage hydrogen replenishment loop, 0053-third-stage hydrogen replenishment loop, 006-foam remover, 007-filter packing layer;

[0031] Figure 2 This is a schematic diagram of a hydrogen replenishment loop pipe according to a specific embodiment of the present invention. In the figure, 005-hydrogen replenishment loop pipe; 0054-hydrogen inlet; 0055-hydrogen inlet;

[0032] Figure 3 This is a schematic diagram of the foam removal mesh of a foam remover according to a specific embodiment of the present invention; 0061 - foam removal mesh;

[0033] Figure 4 This is a schematic diagram of the material diffuser's feeding disc according to a specific embodiment of the present invention. In the diagram, 0033 - feeding circular hole;

[0034] Figure 5The device for processing poor heavy oil by coupling a slurry bed reactor with a catalytic cracking system is shown in the figure, wherein, 1 is a solid-liquid static mixer, 2 is a raw material tank, 3 is a feeding pump, 4 is a heat exchanger, 5 is a hydrogen mixing device, 6 is a heating furnace, 7 is a slurry bed reactor, 8 is a first filter, 9 is a high-pressure separator, 10 is a pressure reducing valve, 8-1 is a second filter, 11 is a fractionating furnace, 12 is a fractionating column, 13 is a liquid material mixer, 14 is a riser catalytic cracker, 15 is a hydrogen circulation compressor, and 16 is a hydrogen compressor buffer tank.

[0035] The specific embodiments of the present application have been shown in the above-mentioned figures, and will be described in more detail hereinafter. The figures and the written description are not intended to limit the scope of the inventive concept in any way, but to illustrate the inventive concept to those skilled in the art by referring to specific embodiments. DETAILED DESCRIPTION

[0036] In order to make the objects, technical solutions and advantages of the present application clearer, the technical solutions in the embodiments will be described clearly and completely in combination with the embodiments of the present application. Obviously, the described embodiments are only some of the embodiments of the present application, but not all the embodiments. Based on the embodiments in the application, all other embodiments obtained by those skilled in the art without any creative work fall within the scope of protection of the present application.

[0037] In the present application, the term "and / or" describes the association relationship of the associated objects, which means that there can be three kinds of relationships, for example, A and / or B can mean that A exists alone, A and B exist together, and B exists alone, wherein A and B can be singular or plural, and the character " / " generally represents an "or" relationship between the associated objects before and after it.

[0038] In the present application, the term "at least one" means one or more, and "multiple" means two or more. "At least one of the following" or similar expressions means any combination of these items, including any combination of single item or multiple items. For example, "at least one of a, b or c", or "at least one of a, b and c", can mean a, b, c, a-b (i.e. a and b), a-c, b-c, or a-b-c, wherein a, b and c can be single or multiple.

[0039] In the present application, the terms "first", "second" are only used for description purpose, to distinguish objects such as substances from each other, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. For example, without departing from the scope of the embodiments of the present application, the first XX can also be referred to as the second XX, and similarly, the second XX can also be referred to as the first XX. Therefore, the features defined with "first", "second" can explicitly or implicitly include one or more of the features.

[0040] In the drawings of the embodiments of the present application, the same or similar reference numerals correspond to the same or similar components; in the description of the present application, it should be understood that, if the orientation or position relationship indicated by the terms "upper", "lower", "left", "right" and the like is based on the orientation or position relationship shown in the drawings, it is only for the convenience of describing the present application and simplifying the description, and does not indicate or imply that the device or component indicated must have a specific orientation, be constructed and operated in a specific orientation, therefore, the terms describing the position relationship in the drawings are only used for exemplary illustration, and cannot be understood as a limitation on the present application, for those skilled in the art, the specific meanings of the above terms can be understood according to the specific circumstances.

[0041] In the present application, unless otherwise explicitly specified and limited, the terms "mounting", "connection", "connecting", "fixing" and the like should be understood in a broad sense, for example, it can be fixed connection, or detachable connection, or integral; it can be mechanical connection, or electrical connection; it can be direct connection, or indirect connection through an intermediate medium, it can be the internal communication of two elements or the interaction relationship between two elements, unless otherwise explicitly limited. For those skilled in the art, the specific meanings of the above terms in the present application can be understood according to the specific circumstances.

[0042] In the description of the present application, the description of the terms "one embodiment", "some embodiments", "a specific embodiment" and the like means that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present application. In the present application, the illustrative description of the above terms does not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described can be combined in any one or more embodiments or examples in a suitable manner.

[0043] In order to provide an inner member type slurry bed reactor which is relatively simple in design, and can strengthen the in-reactor backmixing of reactant flow and inhibit the deposition of coking substances, strengthen heat and mass transfer, and crack heavy oil while separating light components from the system in time, the present application adopts the following technical scheme:

[0044] In a first aspect, the present application provides a slurry bed reactor, which combines Figure 1It is illustrated that the slurry bed reactor comprises a shell, a material inlet 001, a material outlet 002, a hydrogen injection inlet and an inner component; wherein the material outlet 002 is arranged at the top of the shell, the material inlet 001 is arranged at the bottom of the shell, the hydrogen injection inlet is arranged on the surface of the shell, and the inner component is arranged in the shell;

[0045] The inner component is arranged from bottom to top along the axial direction of the shell with a material diffuser 003, a material distributor 004, N-stage hydrogen supplement ring pipes 005 and a material collector; N≥1, the diameter of the hydrogen supplement ring pipe is smaller than the inner diameter of the shell, the pipe wall of the hydrogen supplement ring pipe is provided with at least one hydrogen inlet and a plurality of hydrogen outlets, the opening direction of the hydrogen outlet is upward along the axial direction of the shell; the hydrogen inlet corresponds to and communicates with the hydrogen injection inlet; the material collector communicates with the material outlet.

[0046] In the present application, by arranging the material diffuser 003 and the material distributor 004 in the shell of the slurry bed reactor, the flow form of the material in the slurry bed reactor can be optimized, so that the reaction material can be fully mixed; by arranging the multi-stage hydrogen supplement ring pipe 005, the reaction hydrogen consumption can be supplemented in time and the reaction flow can be lifted, so that the deposition and blockage of the reaction equipment caused by the reaction coke and the excessive cracking of light components caused by the reaction material backmixing can be effectively inhibited; the material collector can collect the material and output the material from the material outlet, so as to avoid the material from falling back due to gravity; the structure of the material collector is not particularly limited in the present application, and the skilled person can directly purchase it, for example, the material collector can be a cap-shaped part with a round hole at the top, a long hole in the side wall and a stainless steel mesh covering it.

[0047] It can be understood that in the above-mentioned inner component, when N is greater than 1, the diameter of each stage of the hydrogen supplement ring pipe is smaller than the inner diameter of the shell, and the pipe wall of each stage of the hydrogen supplement ring pipe is provided with at least one hydrogen inlet and a plurality of hydrogen outlets; at this time, the number of corresponding hydrogen injection inlets is greater than 1, the hydrogen inlet of the pipe wall of each stage of the hydrogen supplement ring pipe corresponds to and communicates with the hydrogen injection inlet (for example, it can communicate through a connecting pipe); in addition, it can be understood that the hydrogen inlet is used to make the external hydrogen enter the slurry bed reactor through the hydrogen supplement ring pipe, and the opening direction of the plurality of hydrogen outlets is upward along the axial direction of the shell, so that the hydrogen can be output upward along the axial direction of the shell, so as to supplement the reaction hydrogen consumption and lift the reaction flow; as for whether the plane where the hydrogen outlet is located is parallel to the axial line of the shell, the present application does not make a particular limitation, for example, when the number of hydrogen outlets is 2, the included angle between the plane where the hydrogen outlet is located and the axial line of the shell is 0°, and when the number of hydrogen outlets is greater than 2, the included angle between the plane where the hydrogen outlet is located and the axial line of the shell is not 0°.

[0048] The present application does not limit the value of N, and the skilled person can set the multi-stage hydrogen supplement loop according to the volume of the slurry bed reactor or the total amount of the material, for example, N is any one of 3, 4, 5, 6, 7, 8, or 9; in a specific embodiment, N = 3, and the N-stage hydrogen supplement loop includes a first-stage hydrogen supplement loop 0051, a second-stage hydrogen supplement loop 0052, and a third-stage hydrogen supplement loop 0053, which are spaced along the axial direction of the shell from bottom to top.

[0049] In a specific embodiment, the diameters of the first-stage hydrogen supplement loop 0051, the second-stage hydrogen supplement loop 0052, and the third-stage hydrogen supplement loop 0053 increase in order.

[0050] In a specific embodiment, the diameters of the first-stage hydrogen supplement loop 0051, the second-stage hydrogen supplement loop 0052, and the third-stage hydrogen supplement loop 0053 increase in order.

[0051] In a specific embodiment, the diameters of the first-stage hydrogen supplement loop 0051, the second-stage hydrogen supplement loop 0052, and the third-stage hydrogen supplement loop 0053 increase in order.

[0052] Further, the hydrogen outlets are arranged at equal intervals along the wall of the hydrogen supplement loop, and the angle between the plane of the hydrogen outlets and the axial direction of the shell is 20°-60°.

[0053] In a specific embodiment, the hydrogen outlets are circular holes arranged at equal intervals, and the diameter and number of the holes are adjusted as needed, for example, 10-20 circular holes with a diameter of 2 cm are arranged at equal intervals along the wall of the hydrogen supplement loop.

[0054] In a specific embodiment, in combination with Figure 2 , the hydrogen supplement loop 005 is provided with two hydrogen inlets 0054 and 0055 for injecting hydrogen into the hydrogen supplement loop from outside the reactor, and the two hydrogen inlets are arranged in a 180° orientation.

[0055] In a specific embodiment, the N-stage hydrogen supplement loop and the material collector further include a foam remover 006 and a filter filler layer 007, and the filter filler layer is used to trap materials with a particle size >100 μm in the filter filler layer. The gaseous hydrocarbons, excess hydrogen, and liquid products generated in the reaction can be efficiently separated by setting the foam remover.

[0056] In a specific embodiment, in combination with Figure 3 , the foam remover includes a foam removal net 0061, which is arranged before the filter filler layer.

[0057] Exemplarily, the filtering filler layer can be arranged between the foam remover and the material collector, and its main purpose is to trap the particles with a particle size greater than 100 μm in the filtering filler layer, and as for its composition, the application is not particularly limited, for example, various types of graded fillers of inert alumina materials available on the market can be selected.

[0058] In a specific embodiment, in combination with Figure 1 , the material diffuser is composed of a material bucket 0031 and a material distribution disc 0032; in combination with Figure 4 , a plurality of material distribution holes 0033 are equidistantly arranged on the surface of the material distribution disc, and the inlet of the material bucket is communicated with or corresponds to the material inlet.

[0059] The material distributor can be a conventional material distributor available on the market, for example, a bubble cap type distributor.

[0060] In a second aspect, the application provides a device for processing poor heavy oil by a slurry bed reactor coupled catalytic cracking system, in combination with Figure 5 , comprising: a solid-liquid static mixer 1, a raw material tank 2, a feed pump 3, a heat exchanger 4, a hydrogen mixing device 5, a heating furnace 6, the slurry bed reactor 7 of the first aspect, a first filter 8, a high-pressure separator 9, a pressure reducing valve 10, a second filter 8-1, a fractionating furnace 11, a fractionating column 12, a liquid material mixing device 13 and a riser catalytic cracking device 14 which are sequentially communicated through first conveying pipelines.

[0061] Among them, the riser catalytic cracking device 14 is communicated with the solid-liquid static mixer 1 through a second pipeline; the hydrogen mixing device 5 is communicated with a hydrogen circulation compressor 15 through a third pipeline, the high-pressure separator 9 is communicated with the heat exchanger 4 through a fourth pipeline, the heat exchanger 4 is communicated with a hydrogen compressor buffer tank 16 through a fifth pipeline, the hydrogen compressor buffer tank 16 is communicated with the hydrogen circulation compressor 15 through a sixth pipeline, and the hydrogen circulation compressor 15 is communicated with a hydrogen injection inlet of the slurry bed reactor 7 through a seventh pipeline.

[0062] The application adopts the coupling process idea of “staged reaction + circulating reaction + unified catalytic system”, realizes the continuous and stable operation of the processing device under the premise of ensuring the high conversion rate of poor oil, realizes the deep conversion of poor oil and the goal of producing more chemical raw materials and light motor fuel oil, and in detail, the slurry bed reactor and the riser catalytic cracking device of the application use the same catalyst, the equilibrium agent and the waste catalyst discharged from the riser catalytic cracking device can be used for the slurry bed reactor system, which is beneficial to exert the cracking activity of the catalytic cracking catalyst and improve the cracking depth of the poor heavy oil, and in addition, the reaction coke of the slurry bed reactor also enters the regenerator of the riser catalytic cracking device together with the hydrogenated tail oil to complete the coke burning and removal.

[0063] The first filter and the second filter are mainly used to remove coke particles with a particle size of >50 μm, and the specific composition of the filters is not limited in the present application.

[0064] The fractionating column 12 is exemplarily a normal pressure column and a vacuum column, the riser catalytic cracking device 14 is a riser catalytic cracking system, and the solid-liquid static mixer is a commercially available solid-liquid static mixer.

[0065] In a third aspect, the present application provides a method for treating inferior heavy oil by using the device, which comprises the following steps:

[0066] 1) The equilibrium agent, the catalyst and the inferior heavy oil to be treated are mixed in the solid-liquid static mixer 1 to obtain a mixture, and the mixture is input into the raw material tank 2, and after being stabilized for a certain time, the mixture is pumped into the heat exchanger 4 for heat exchange;

[0067] 2) The mixture after heat exchange is input into the hydrogen mixing device 5, the hydrogen gas output by the hydrogen circulation compressor 15 is mixed with the mixture in the hydrogen mixing device 5, and then the mixture is input into the heating furnace 6 for heating, and then the mixture is input into the slurry bed reactor 7 for inferior heavy oil conversion reaction to obtain a hydrocracking product;

[0068] 3) The hydrocracking product is input into the high-pressure separator 9 after removing the reaction coke particles with a particle size of >50 μm by the first filter 8, and the gas-liquid separation is completed, wherein the gas phase product is input into the hydrogen gas compressor buffer tank 16 after heat exchange by the heat exchanger 4, and then the gas phase product is input into the hydrogen circulation compressor 15, the liquid phase product is input into the second filter 8-1 to remove the remaining reaction coke particles with a particle size of >50 μm, and then the liquid phase product is input into the fractionating furnace 11, and after being heated by the fractionating furnace, the liquid phase product is input into the fractionating column 12 for fractionation to obtain gasoline, diesel, light wax oil and hydrogenated tail oil with an initial boiling point of 450-500°C;

[0069] 4) The hydrogenated tail oil and the oil slurry to be catalytically cracked are input into the liquid material mixer 13, mixed, and then input into the riser catalytic cracking device 14 for catalytic cracking to obtain dry gas, liquefied gas, gasoline, diesel, catalytically cracked oil slurry, and unloaded equilibrium agent and catalyst;

[0070] 5) The catalytically cracked oil slurry, the unloaded equilibrium agent and the catalyst are input into the solid-liquid static mixer 1 to be recycled to steps 1)-4).

[0071] In the above method, step 4) selects the hydrocracking tail oil with the initial boiling point of 450-500℃ as the input liquid material mixer, that is, a certain amount of hydrocracked gas oil is contained in the hydrocracking tail oil, which is beneficial to the normal cracking reaction of the catalytic cracking system, and the slurry bed hydrocracking tail oil and the fresh raw material to be catalytically cracked are mixed into the catalytic cracking system for reaction, and the residual coke contained in the hydrocracking tail oil can be burned and removed in the regenerator of the catalytic cracking system. In addition, it can be understood that the catalytic cracking oil slurry of step 4) is the cracking reaction residue, which is the heavy oil component that has not undergone cracking reaction.

[0072] The above method uses the process coupling of the slurry bed reactor and the riser catalytic cracker to realize step-by-step cracking and cyclic cracking, and finally realizes the deep conversion of poor quality oil and the goal of producing more chemical raw materials and light vehicle fuel oil. It can be understood that the above method circulates a batch of equilibrium agent and catalyst, that is, the same catalyst is used in the slurry bed reactor and the riser catalytic cracker, and the equilibrium agent and waste catalyst discharged from the riser catalytic cracker of step 5) are used again in the slurry bed reactor, which is beneficial to the cracking activity of the catalytic cracking catalyst and improves the cracking depth of poor quality heavy oil.

[0073] Illustratively, the poor quality heavy oil to be treated is at least one of a mixture of high-sulfur residual oil, high-metal residual oil, atmospheric residual oil, vacuum residual oil, super-viscous crude oil, catalytic oil slurry, oil sand bitumen and the like.

[0074] In a specific embodiment, the operating parameters of the slurry bed reactor 7 are as follows: the reaction temperature is 390-405℃, the reaction pressure is 12.0-14.0 MPa, the volume space velocity is 0.5-1.0 h-1, and the hydrogen oil volume ratio is 500-800.

[0075] In a specific embodiment, in step 1), the mass ratio of the equilibrium agent to the catalyst is 70-80:20-30. The catalyst and the equilibrium agent can be commonly used catalytic cracking catalysts on the market, and the present application is not particularly limited, such as silicon-aluminum catalyst, molecular sieve catalyst and the like, and further is the catalytic cracking catalyst with the trade name LV-23 of Lanzhou Petrochemical Catalyst Factory.

[0076] In a specific embodiment, when N≥2, the hydrogen supplement amount of the first-stage hydrogen supplement loop is 1-5% of the hydrogen feed amount of the hydrogen mixer 5, and the hydrogen supplement amount of the N-stage hydrogen supplement loop is 1.1-1.5 times of the hydrogen supplement amount of the N-1-stage hydrogen supplement loop. In this embodiment, better hydrogen supplement effect can be achieved, thereby better inhibiting the deposition and plugging of the reaction coke and the over-cracking of light components caused by the reaction material backmixing.

[0077] The present application is further described below in conjunction with specific embodiments:

[0078] The following test involves the raw material or equipment source information is shown in the following table 1:

[0079] Table 1:

[0080]

[0081] The following test involves the evaluation analysis as shown in the following table 2.

[0082] Table 2:

[0083] Name Analytical method / National standard Analytical method / ASTM method Density GB / T 1884 ASTM D4052 Sulfur content — ASTM D5453 Nitrogen content — ASTM D5762 Metal content (ICP method) — ASTM D5708-05 Carbon residue GB / T 17144 — Simulated distillation — ASTM 7169 Toluene insoluble — — True boiling point distillation — ASTM D2892

[0084] Example 1

[0085] This example provides a slurry bed reactor, combined Figure 1 , including: shell (outer diameter 300mm);

[0086] Material inlet 001, provided at the bottom of the shell;

[0087] Material outlet 002, provided at the top of the shell;

[0088] Hydrogen injection port, provided on the surface of the shell;

[0089] And the inner member is provided in the shell;

[0090] The inner member is provided with a material diffuser 003, a material distributor 004, N-stage hydrogen supplement ring pipe 005, a foam remover 006, a filter filler layer 007 and a material collector along the axial direction of the shell from bottom to top; wherein N=3, including a first-stage hydrogen supplement ring pipe 0051, a second-stage hydrogen supplement ring pipe 0052 and a third-stage hydrogen supplement ring pipe 0053 distributed along the axial direction of the shell from bottom to top, two hydrogen injection ports are provided at each stage, hydrogen is injected into the hydrogen supplement ring pipe from the outside of the reactor, the two hydrogen injection ports are oppositely arranged at an angle of 180 degrees, the hydrogen injection ports correspond to and communicate with the hydrogen injection ports; circular holes are opened on each hydrogen supplement ring pipe at equal intervals, the opening direction is upward along the axial direction of the reactor, the included angle between the plane of the circular hole and the axial direction of the shell is shown in Table 4, and four circular holes (two groups) are provided on each hydrogen supplement ring pipe; the material diffuser is composed of a distribution barrel and a distribution disc; a plurality of circular holes are equidistantly arranged on the surface of the distribution disc, and the inlet of the distribution barrel communicates with or corresponds to the material inlet.

[0091] The material distributor is a bubble cap type distributor; the foam remover includes a foam removal net 0061 (see Figure 3 );

[0092] The filter filler layer includes a fixed filter filler bed layer formed by stacking tooth balls, the outer diameter of the tooth ball is 1-3mm, the pore volume is >0.7, and the rich microporous structure can adsorb solid particulate matter.

[0093] Examples 2-6

[0094] A slurry bed reactor is provided respectively, and the differences from Example 1 are shown in Table 4.

[0095] Comparative Example 1

[0096] A slurry bed reactor is provided respectively, and the differences from Example 1 are shown in Table 4.

[0097] Test Example 1

[0098] An apparatus for processing inferior heavy oil by coupling 7 kinds of slurry bed reactors with catalytic cracking system is provided, which respectively comprises the slurry bed reactors of Examples 1-6 and Comparative Example 1, and is combined with Figure 5 , and specifically comprises, in sequence through a first conveying pipeline, a solid-liquid static mixer 1, a raw material tank 2, a feeding pump 3, a heat exchanger 4, a hydrogen mixing device 5, a heating furnace 6, a slurry bed reactor 7, a first filter 8, a high-pressure separator 9, a pressure reducing valve 10, a second filter 8-1, a fractionating furnace 11, a fractionating column 12, a liquid material mixing device 13, and a riser catalytic cracking device 14.

[0099] The riser catalytic cracking device 14 is connected with the solid-liquid static mixer 1 through a second pipeline; the hydrogen mixing device 5 is connected with a hydrogen circulation compressor 15 through a third pipeline, the high-pressure separator 9 is connected with the heat exchanger 4 through a fourth pipeline, the heat exchanger 4 is connected with a hydrogen compressor buffer tank 16 through a fifth pipeline, the hydrogen compressor buffer tank 16 is connected with the hydrogen circulation compressor 15 through a sixth pipeline, and the hydrogen circulation compressor 15 is connected with a hydrogen injection inlet of the slurry bed reactor 7 through a seventh pipeline.

[0100] Test Example 2

[0101] A method for processing inferior heavy oil by using the 7 kinds of apparatuses of Test Example 1 respectively is provided, which comprises the following steps:

[0102] 1) The balancing agent, the catalyst, and the inferior heavy oil to be processed are mixed in the solid-liquid static mixer 1 to obtain a mixed material, which is then input into the raw material tank 2 and stabilized for a certain period of time before being pumped into the heat exchanger 4 for heat exchange;

[0103] 2) The mixed material after heat exchange is input into the hydrogen mixing device 5, hydrogen output by the hydrogen circulation compressor 15 is mixed with the mixed material in the hydrogen mixing device 5, and then input into the heating furnace 6 for heating, and then input into the slurry bed reactor 7 for inferior heavy oil conversion reaction to obtain a hydrocracking product;

[0104] 3) The hydrocracking product is input into a high-pressure separator 9 after removing the reaction coke particles with a particle size greater than 50 μm through a first filter 8 to complete gas-liquid separation, wherein the gas phase product is input into a hydrogen circulating compressor 15 after heat exchange through a heat exchanger 4 and input into a hydrogen compressor buffer tank 16, the liquid phase product is input into a second filter 8-1 to remove the remaining reaction coke particles with a particle size greater than 50 μm again, and is input into a fractionating furnace 11 after heating through the fractionating furnace and is input into a fractionating column 12 to obtain gasoline, diesel, light wax oil and hydrogen tail oil with an initial boiling point of 450-500 ℃ after fractionation;

[0105] 4) The hydrogen tail oil is mixed with the oil slurry to be catalytically cracked in a liquid material mixer 13, and is input into a riser catalytic cracker 14 after mixing to obtain dry gas, liquefied gas, gasoline, diesel, catalytic cracking oil slurry, and discharged equilibrium agent and catalyst;

[0106] 5) The catalytic cracking oil slurry, the discharged equilibrium agent and the catalyst are input into a solid-liquid static mixer 1 to circulate steps 1)-4) again.

[0107] The oil slurry to be catalytically cracked is prepared by mixing Venezuela vacuum residue, Karamay vacuum residue and West Pacific vacuum residue, and the properties are shown in Table 3, the catalytic cracking catalyst used is LV-23, the process conditions are shown in Table 4, and the test results are shown in Table 5, wherein the conversion rate of poor heavy oil = (gasoline + diesel + light wax oil) / (gasoline + diesel + light wax oil + hydrogen tail oil + toluene insoluble) · 100%.

[0108] Table 3 Properties of raw oil

[0109]

[0110]

[0111] Table 4 Operating conditions of examples and comparative examples

[0112]

[0113]

[0114] In the table, "times" refers to the times of the hydrogen make-up amount of the hydrogen make-up loop at this stage compared with the hydrogen make-up amount of the hydrogen make-up loop at the previous stage, or the times of the diameter of the hydrogen make-up loop at this stage compared with the diameter of the hydrogen make-up loop at the previous stage, and "-" refers to that this example does not have this parameter.

[0115] Table 5 Test results

[0116]

[0117]

[0118] According to the product distribution of the slurry bed, under the same equipment and process conditions, the conversion rate is 94.7%, the gasoline yield is 30.1%, and the diesel yield is 35.2% when the hydrogen supplement loop reactor is used; and the conversion rate is 82.1%, the gasoline yield is 13.5%, and the diesel yield is 22.3% when the hydrogen supplement loop reactor is not used; therefore, the application has obvious advantages, and the test results of the application are better than those of the slurry bed reaction without hydrogen supplement loop in terms of the removal rates of sulfur, nitrogen, residual carbon, metal and other impurities.

[0119] Secondly, within the test operation condition range of the examples and the comparative examples, with the increase of the hydrogen supplement loop stage number, the hydrogen supplement loop opening group number, the included angle between two adjacent hydrogen supplement openings, and the severity of the reaction conditions, the density of the reaction product gradually decreases, the impurity removal rate increases, the gasoline and diesel yields increase, and the light hydrocarbon and oil slurry yields gradually decrease.

[0120] Finally, it should be noted that the above examples are only used to illustrate the technical solutions of the application, and not to limit the application; although the application has been described in detail with reference to the above examples, those skilled in the art should understand that the technical solutions described in the above examples can still be modified, or some or all of the technical features can be replaced by equivalents; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the examples of the application.

Claims

1. A slurry bed reactor characterized by, include: The enclosure comprises a shell, a material outlet, a material inlet, a hydrogen injection port, and internal components; wherein the material outlet is located at the top of the shell, the material inlet is located at the bottom of the shell, the hydrogen injection port is located on the surface of the shell, and the internal components are located inside the shell. The internal components are arranged from bottom to top along the axial direction of the shell, including a material diffuser, a material distributor, an N-stage hydrogen replenishment loop, and a material collector; N≥1, the diameter of the hydrogen replenishment loop is smaller than the inner diameter of the shell, the tube wall of the hydrogen replenishment loop is provided with at least one hydrogen inlet and several hydrogen outlets, the opening direction of the hydrogen outlets is upward along the axial direction of the shell; the hydrogen inlets correspond one-to-one with the hydrogen injection ports and are connected; the material collector is connected to the material outlets.

2. The slurry bed reactor of claim 1, wherein, The N-stage hydrogen replenishment loop includes a primary hydrogen replenishment loop, a secondary hydrogen replenishment loop, and a tertiary hydrogen replenishment loop that are spaced apart from bottom to top along the axial direction of the shell. And / or, the diameters of the primary hydrogen replenishment loop, the secondary hydrogen replenishment loop, and the tertiary hydrogen replenishment loop increase in that order; And / or, the number of hydrogen outlets in the primary hydrogen replenishment loop, the secondary hydrogen replenishment loop, and the tertiary hydrogen replenishment loop increases in that order.

3. The slurry bed reactor of claim 2, wherein, The hydrogen outlets are evenly spaced along the wall of the hydrogen replenishment ring pipe, and the plane where the hydrogen outlets are located makes an angle of 20° to 60° with the axial direction of the shell.

4. The slurry bed reactor according to claim 1, characterized in that, The material diffuser consists of a material distribution bucket and a material distribution tray; the surface of the material distribution tray has several circular holes arranged at equal intervals, and the inlet of the material distribution bucket is connected to or corresponds to the material inlet.

5. The slurry bed reactor according to claim 1, characterized in that, The N-stage hydrogen replenishment loop and the material collector also include a foam remover and a filter packing layer, which is used to retain materials with a particle size >100μm within the filter packing layer.

6. A device for processing low-quality heavy oil using a slurry bed reactor coupled with a catalytic cracking system, characterized in that, include: The solid-liquid static mixer, raw material tank, feed pump, heat exchanger, hydrogen mixer, heater, slurry bed reactor as described in any one of claims 1-5, first filter, high-pressure separator, pressure reducing valve, second filter, fractionating furnace, fractionating tower, liquid material mixer and riser catalytic cracker are sequentially connected through the first conveying pipeline. The riser catalytic cracker is connected to the solid-liquid static mixer via a second pipe; the hydrogen mixer is connected to the hydrogen recirculation compressor via a third pipe; the high-pressure separator is connected to the heat exchanger via a fourth pipe; the heat exchanger is connected to the hydrogen compressor buffer tank via a fifth pipe; the hydrogen compressor buffer tank is connected to the hydrogen recirculation compressor via a sixth pipe; and the hydrogen recirculation compressor is connected to the hydrogen injection port of the slurry bed reactor via a seventh pipe.

7. A method for treating inferior heavy oil using the apparatus of claim 6, characterized in that, Includes the following steps: 1) The balancer, catalyst and the inferior heavy oil to be treated are mixed in a solid-liquid static mixer to obtain a mixture. The mixture is fed into the raw material tank and stabilized for a certain period of time before being pumped into the heat exchanger for heat exchange. 2) After heat exchange, the mixture is fed into the hydrogen mixer. The hydrogen output from the hydrogen circulation compressor is mixed with the mixture in the hydrogen mixer and then fed into the heating furnace for heating. After that, it is fed into the slurry bed reactor for the conversion reaction of inferior heavy oil to obtain hydrocracking products. 3) After the hydrocracking products are filtered to remove reactive coke particles with a particle size >50μm, they are fed into a high-pressure separator to complete gas-liquid separation. The gas phase products are heated by a heat exchanger and then fed into the hydrogen compressor buffer tank, and then into the hydrogen recirculation compressor. The liquid phase products are filtered to remove the remaining reactive coke particles with a particle size >50μm by a pressure reducing valve and then fed into a fractionating furnace. After being heated in the fractionating furnace, they are fed into a fractionating tower for fractionation to obtain gasoline, diesel, light wax oil and hydrocracking tail oil with an initial boiling point of 450-500℃. 4) The hydrotreated tail oil and the slurry to be catalytically cracked are fed into a liquid material mixer, mixed, and then fed into a riser catalytic cracking reactor for catalytic cracking reaction to obtain dry gas, liquefied petroleum gas, gasoline, diesel, catalytic cracking slurry, and unloaded balance agent and catalyst. 5) The catalytic cracking slurry, the discharged balance agent, and the catalyst are fed back into the solid-liquid static mixer for recirculation of steps 1)-4).

8. The method according to claim 7, characterized in that, The operation parameters of the slurry bed reactor are as follows: reaction temperature is 390-405℃, reaction pressure is 12.0-14.0MPa, volume space velocity is 0.5-1.0h -1 , and hydrogen / oil volume ratio is 500-800.

9. The method according to claim 7, characterized in that, In step 1), the mass ratio of the balancing agent to the catalyst is 70-80:20-30.

10. The method according to claim 7, characterized in that, When N≥2, the hydrogen supply of the first-stage hydrogen supply loop is adjusted to 1-5% of the hydrogen feed rate of the hydrogen mixer, and the hydrogen supply of the N-stage hydrogen supply loop is 1.1-1.5 times that of the N-1 stage hydrogen supply loop.

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