Three-phase separator and fluidized bed reactor using the same

Abstract

The present invention discloses a three-phase separator and an ebullating bed reactor using the separator. The three-phase separator includes: a central guide tube, which receives gas-liquid materials and solid catalyst particles carried upward from the bottom of the reactor, and forms a first deflection of liquid-solid materials at the top; an outer guide tube, which is sleeved on the outside of the central guide tube, and the liquid-solid materials after the first deflection descend in the annular space between the outer guide tube and the reactor wall; an overflow deflector, which is sleeved between the central guide tube and the outer guide tube, and forms a separation of liquid-solid materials and a second deflection of liquid-phase materials at the lower end of the overflow deflector; a third deflection of liquid-phase materials is formed at the upper end of the overflow deflector, and the liquid-phase materials that have been deflected and descended for the third time are discharged from the liquid outlet pipe located at the lower part of the outer wall of the overflow deflector. The present invention can effectively avoid the influence of rising gas on the liquid-solid separation efficiency through the structural design of the paperclip-type reverse sequence built-in three-phase separator.

Description

Technical Field

[0001] The present invention relates to the technical field of gas-liquid-solid separation, in particular to a gas-liquid-solid three-phase separator and a fluidized bed reactor using the separator. Background Art

[0002] An ebullated-bed reactor generally requires a gas-liquid-solid three-phase separator located in the upper portion of the reactor. The liquid phase in the ebullated bed is the continuous phase, while the gas phase bubbles through the reactor, driven by the gas. The solid phase is the dispersed phase. Ebullated-bed reactors typically feature an online catalyst addition and removal system. During operation, the reactor pressure drop is relatively stable, making them particularly suitable for hydrotreating low-quality residual oils. The residual oil feedstock has a high content of impurities, resulting in a highly exothermic reaction and rapid catalyst poisoning and deactivation. Regular online catalyst replacement and solid phase circulation within the reactor via a three-phase separator ensure stable reaction systems and long-term operation.

[0003] The existing three-phase separator is equipped with multiple annular cylinders in the upper part of the reactor. Figure 1 As shown, the gas-liquid-solid mixture ascends within the annular inner tube, completing gas-phase separation at the upper gas-liquid interface. The liquid-solid mixed fluid overflows to the surrounding areas and descends into the area between the outer and inner annular tubes. Based on the solid-liquid density difference in the annular area between the outer annular tube and the reactor wall, the solids flow downward with the liquid out of the separator and return to the main reaction zone for circulation. The remaining liquid phase, operating under the "U"-shaped tube principle, flows upward through the annular gap between the annular outer tube and the reactor wall through the discharge pipe and out of the reactor. Specifically, a gas phase outflow channel is provided at the top of the reactor, while the liquid phase overflows out of the reactor through a side opening. The solid catalyst flows out of the separator due to gravity differences in the liquid phase, achieving three-phase separation. This type of three-phase separator is called a straight-tube or expanded-sequential built-in three-phase separator.

[0004] For example, Chinese patent application CN101376092A discloses an ebullated bed reactor comprising a cylindrical reactor shell perpendicular to the ground, a three-phase separator in the upper portion of the shell, and a guide structure in the upper portion of the reactor. The guide structure is an annular protrusion disposed on the inner wall of the reactor, and its longitudinal cross-section along the reactor axis is trapezoidal or arcuate. The installation of the guide structure and its integration with the three-phase separator increase the operational flexibility of the three-phase separator, ensuring efficient separation and significantly reducing catalyst carryover. However, this type of existing sequential built-in three-phase separator still has a certain amount of gas phase inflow at the liquid-solid deflection position, and the bubble tail vortex effect will cause disorder in the catalyst particles, affecting the solid-liquid separation effect; millimeter-level bubbles rise faster, and hundred-micron-level bubbles rise slower and will be affected by larger bubbles to move disorderly in the radial direction. At present, there are basically millimeter-level bubbles in the boiling bed reactor. In order to reduce the impact of bubbles entering in the vertical direction on separation and prevent gas from rising, the aforementioned guide structure is added to the straight-cylinder reactor, or the inner diameter of the reactor is expanded at the built-in separator position, that is, an expanded sequential built-in three-phase separator is adopted to make the gas phase rise vertically and avoid the deflection area as much as possible. Although it can play a certain role, liquid-solid separation still cannot avoid the influence of rising gas, and this structural design is relatively complex and the investment is high.

[0005] Therefore, there is an urgent need for a gas-liquid-solid three-phase separator and an ebullated bed reactor using the separator, so as to effectively avoid the influence of rising gas on the liquid-solid separation efficiency.

[0006] The information disclosed in this background technology section is only intended to enhance understanding of the overall background of the invention and should not be regarded as an admission or any form of suggestion that the information constitutes the prior art already known to a person skilled in the art. Summary of the Invention

[0007] The purpose of the present invention is to provide a three-phase separator and an ebullated bed reactor using the separator. Through the structural design of the paperclip-type reverse-sequence built-in three-phase separator, the influence of rising gas on the liquid-solid separation efficiency can be effectively avoided.

[0008] To achieve the above-mentioned purpose, according to the first aspect of the present invention, a three-phase separator is provided, which is arranged in a fluidized bed reactor and is used for gas-liquid-solid three-phase separation, comprising: a central guide tube, which receives gas-liquid materials and solid catalyst particles carried upward from the bottom of the reactor, and forms a first deflection of liquid-solid materials at the top; an outer guide tube, which is sleeved on the outside of the central guide tube, and the liquid-solid materials after the first deflection descend in the annular space between the outer guide tube and the reactor wall; an overflow deflector tube, which is sleeved between the central guide tube and the outer guide tube, and forms liquid-solid material separation and a second deflection of liquid materials at the lower end of the overflow deflector tube; a third deflection of liquid materials is formed at the upper end of the overflow deflector tube, and the liquid materials that have been deflected and descended for the third time are discharged from the liquid outlet pipe located at the lower part of the outer wall of the overflow deflector tube.

[0009] Furthermore, in the above technical solution, the top end of the central guide tube is connected to the top end of the outer guide tube via an upper sealing baffle, and the upper sealing baffle is located above the top end of the overflow deflector tube and is arranged obliquely.

[0010] Furthermore, in the above technical solution, the central guide tube includes an upper straight tube section and a lower expansion section.

[0011] Furthermore, in the above technical solution, the liquid phase material after the third deflection can be discharged to the liquid outlet pipe through the diversion buffer unit.

[0012] Furthermore, in the above technical solution, the diversion buffer unit may include: a curved baffle, which extends downward from the inner wall of the outer guide tube, and is used to alleviate the excessive suction of liquid materials after the third deflection; a diversion buffer baffle, which is arranged at the bottom of the annular space between the outer guide tube and the overflow deflection tube, and is arranged downward from the far end to the proximal end of the liquid outlet pipe, and is used to receive the drainage from the curved baffle and uniformize the liquid flow rate in the annular space at the liquid outlet pipe.

[0013] Furthermore, in the above technical solution, an anti-deposition portion may be provided at the bottom of the diversion buffer baffle, which is integrally formed with the diversion buffer baffle and is an annular inflation space with a closed bottom. The diversion buffer baffle serves as the upper cover of the annular inflation space and air holes are evenly opened at corresponding positions of the upper cover. By inflating the annular inflation space, bubbles generated at the air holes form turbulence for the liquid material on the diversion buffer baffle.

[0014] Furthermore, in the above technical solution, the inclination angle of the annular section of the upper end of the curved baffle can be 110° to 120°; the inclination angle of the diversion buffer baffle can be 5° to 20°.

[0015] Furthermore, in the above technical solution, an exhaust pipe may be provided above the third deflection position and at the connection between the upper sealing baffle and the central guide tube, wherein the exhaust pipes are arranged in a circular array, and the outlet of the exhaust pipe is located above the liquid level of the reactor.

[0016] According to a second aspect of the present invention, the present invention provides an ebullated bed reactor, wherein any one of the above-mentioned three-phase separators is arranged in the ebullated bed reactor.

[0017] Furthermore, in the above technical solution, the reactor shell is a straight cylindrical structure, a gas outlet pipe is provided at the top center of the upper head of the straight cylindrical structure, and a feed port is provided at the bottom center of the lower head of the straight cylindrical structure; the three-phase separator is provided in the upper space inside the reactor shell.

[0018] Furthermore, in the above technical solution, a gas-liquid distributor is provided in the lower space of the reactor shell and below the catalyst bed.

[0019] Furthermore, in the above technical solution, a solid catalyst particle filling port may be provided at the upper end cap; and a solid catalyst particle discharge port may be provided at the lower end cap.

[0020] Furthermore, in the above technical solution, a guide portion may be provided at a corresponding position on the lower end of the expansion section of the central draft tube of the three-phase separator. The guide portion is an annular protrusion structure or a folded plate structure provided along the circumference of the inner wall of the reactor.

[0021] Compared with the prior art, the present invention has the following beneficial effects:

[0022] 1) The present invention achieves a "reverse order" (i.e., a paper clip-like direction) of material flow through a "three-tube sleeve" structural design, increases the radial travel of the first and second deflections, and allows the material flowing upward from the central guide tube to be directly deflected to the annular space between the outer guide tube and the reactor wall. As a result, the radial travel of the second deflection is also effectively increased compared to the "sequential" material flow in the prior art, making it less likely for gas to rise in the liquid-solid separation zone. In addition, since the present invention adopts a "reverse order" material flow, even if some bubbles have an upward trend, since their upward path is opposite to the path of the liquid out of the reactor, it is not easy for the solid phase to flow out of the reactor with the liquid phase. The inventors have shown through experiments that when using the straight-cylinder reactor of the present invention, the effect of preventing bubbles from rising is better than that of the existing expanded reactor (i.e., a design with a larger radial dimension of the reactor at the three-phase separator). Based on the fluid mechanics principle that bubbles tend to rise in a straight line, the "reverse order" of the material flow in the present invention and the "sequential order" in the prior art achieve the interchange of the two deflection zones, which can effectively prevent bubbles from entering the liquid-solid separation space and interfering with the fine separation of liquid and solid, thereby effectively maintaining the long-term stability of the separation efficiency of the three-phase separator.

[0023] 2) To address the uneven outflow from the annular gap, the present invention discharges the liquid material after the third deflection through a diversion buffer unit to the liquid outlet pipe. The diversion buffer unit's curved baffle extends downward from the inner wall of the outer guide tube, effectively alleviating the overly rapid inhalation of the liquid material after the third deflection. By positioning the diversion buffer baffle at the bottom of the annular space between the outer guide tube and the overflow deflector tube, and slanting downward from the distal end to the proximal end of the liquid outlet pipe, it receives drainage from the curved baffle and effectively evens out the liquid flow rate in the annular space at the liquid outlet pipe.

[0024] 3) The anti-deposition portion of the present invention is an annular space located below the guide buffer baffle for generating bubbles. After the annular space is filled with gas, the bubbles can be controlled to enter the liquid outflow area. The generated bubbles can enhance the turbulence of the liquid at the guide buffer baffle, thereby preventing coking.

[0025] 4) The guide portion of the present invention can be configured as a raised or baffle-shaped structure. This guide portion needs to withstand pressure under high-pressure conditions. Therefore, compared to an annular raised structure, a baffle-shaped structure is less pressure-resistant and is therefore preferred. This structure minimizes abrasion of catalyst particles, given that bubbles coalesce between the baffle and the reactor wall, forming large bubble cavities and a certain level of contact between the gas and liquid films.

[0026] The above description is only an overview of the technical solution of the present invention. In order to more clearly understand the technical means of the present invention and to implement it according to the contents of the specification, and to make the above and other purposes, technical features and advantages of the present invention easier to understand, one or more preferred embodiments are listed below and described in detail with reference to the accompanying drawings. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 This is a structural schematic diagram of a straight-cylinder sequential built-in three-phase separator in an existing fluidized bed reactor (showing the inner and outer cylinder structures of the existing three-phase separator and the flow of materials).

[0028] Figure 2 It is a schematic cross-sectional view of the straight-cylinder reverse-sequence built-in three-phase separator of the present invention.

[0029] Figure 3 It is a perspective three-dimensional structural diagram of the three-phase separator of the present invention.

[0030] Figure 4 It is a schematic diagram of the three-dimensional structure of the guide buffer baffle and the anti-deposition part of the three-phase separator of the present invention.

[0031] Figure 5 It is a schematic cross-sectional structural diagram of the ebullating bed reactor of the present invention.

[0032] Figure 6It is a perspective three-dimensional structural diagram of the ebullated bed reactor of the present invention.

[0033] Description of main reference numerals:

[0034] Figure 1 In the figure, 1A-inner cylinder, 2A-outer cylinder, 3A-liquid outlet pipe, 4A-gas outlet pipe; 100A-existing ebullating bed reactor;

[0035] Figures 2 to 6 In the figure, 1-central guide tube, 11-straight section, 12-expansion section, 2-outer guide tube, 3-overflow deflector tube, 4-upper sealing baffle, 5-curved baffle, 6-guide buffer baffle, 60-air hole, 61-air filling space of anti-deposition part, 62-air filling pipe, 7-liquid outlet pipe, 8-exhaust pipe; 100-ebullated bed reactor, 101-reactor shell, 102-folded plate, 103-gas outlet pipe, 104-feed port, 105-gas-liquid distributor, 106-solid catalyst particle filling port, 107-solid catalyst particle discharge port;

[0036] Figure 5 In the figure, A is the solid catalyst particle bed, and B is the reactor liquid level. DETAILED DESCRIPTION

[0037] The specific embodiments of the present invention are described in detail below with reference to the accompanying drawings, but it should be understood that the protection scope of the present invention is not limited by the specific embodiments.

[0038] Unless expressly stated otherwise, throughout the specification and claims, the term “comprise” or variations such as “include” or “comprising” will be understood to include the stated elements or components but not to exclude other elements or components.

[0039] In this document, for ease of description, spatially relative terms such as "below," "beneath," "below," "above," "above," etc. may be used to describe the relationship of one element or feature to another element or feature in the accompanying drawings. It should be understood that the spatially relative terms are intended to encompass different orientations of the object in use or operation in addition to the orientation depicted in the drawings. For example, if the object in the drawings is turned over, the element described as being "below" or "beneath" other elements or features will be oriented "above" the elements or features. Therefore, the exemplary term "below" can include both below and above. Objects may also have other orientations (rotated 90 degrees or other orientations) and the spatially relative terms used herein should be interpreted accordingly.

[0040] In this document, the terms "first", "second", etc. are used to distinguish two different elements or parts, and are not used to limit specific positions or relative relationships. In other words, in some embodiments, the terms "first", "second", etc. can also be interchangeable with each other.

[0041] The three-phase separator of the present invention is for Figure 1 Improvements made to the prior art shown. Figure 1 A conventional fluidized bed reactor 100A is shown, which is used for gas-liquid-solid three-phase reactions. A gas-liquid mixed feed from the bottom of the reactor contacts solid catalyst particles disposed in the lower middle portion of the reactor, causing a catalytic reaction. The gas, liquid, and solid phases continue to ascend and are directed into a three-phase separator consisting of an inner tube 1A and an outer tube 2A. This conventional three-phase separator is located in the upper middle portion of the reactor and is used for gas-liquid-solid three-phase separation. The material flow in this conventional three-phase separator is as follows: the gas-liquid-solid mixture ascends within the annular inner tube 1A, completing gas-phase separation at the upper gas-liquid interface. The liquid-solid mixed fluid overflows to the surrounding area and descends into the area between the outer tube 2A and the inner tube 1A. In the annular region between the outer tube 2A and the reactor wall, due to the solid-liquid density difference, the solids flow downward with the liquid out of the three-phase separator and return to the main reaction zone for circulation. The remaining liquid phase, operating under the "U"-shaped tube principle, flows upward through the annular gap between the annular outer tube 2A and the reactor wall, out of the reactor through a discharge pipe 3A. That is, a gas phase outflow channel 4A is set at the top of the reactor, and the liquid phase overflows from the discharge pipe 3A at the side opening to the reactor 100A. The solid catalyst flows out of the separator under the action of gravity difference in the liquid phase, thus achieving three-phase separation. This existing three-phase separator is a straight-cylinder sequential type built-in three-phase separator. The so-called "sequential type" is referred to as Figure 1 The direction of the arrow at the three-phase separator indicates that the material ascends along the inner cylinder 1A, then descends into the annular space between the inner cylinder 1A and the outer cylinder 2A. After liquid-solid separation, the liquid phase ascends along the annular space between the outer cylinder 2A and the reactor wall, and overflows out of the reactor 100A when it reaches the discharge pipe 3A. The present invention improves upon the above-mentioned existing three-phase separator by the following: Example 1

[0042] like Figure 2 、 3As shown, this embodiment provides a three-phase separator with a "reverse-type" structural design, which is arranged in the shell 101 of the fluidized bed reactor and is used for gas-liquid-solid three-phase separation. The three-phase separator includes: a central guide tube 1, an outer guide tube 2, and an overflow deflection tube 3. Among them, the central guide tube 1 receives the gas-liquid materials and the solid catalyst particles carried upward from the bottom of the reactor 100, and forms a first deflection of the liquid and solid materials at the top (the gas phase has been separated at the liquid surface B of the reactor). The outer guide tube 2 is arranged on the outside of the central guide tube 1, and the liquid and solid materials after the first deflection descend in the annular space between the outer guide tube 2 and the reactor wall. The overflow deflector 3 is sleeved between the central guide tube 1 and the outer guide tube 2. The liquid-solid material separation and the second deflection of the liquid phase material are formed at the lower end of the overflow deflector 2 (U-tube principle); the upward liquid phase material forms a third deflection at the upper end of the overflow deflector 2. The liquid phase material that has undergone the third deflection and descended is discharged from the liquid outlet pipe 7 located at the lower part of the outer wall of the overflow deflector 2. Compared with the existing technology, this embodiment adopts a "three-tube sleeve" structure and changes the direction of the material (see Figure 2 ), the material direction is similar to a "paper clip", which is significantly different from the existing "sequential" material direction. The material direction of this embodiment adopts a "reverse" material direction based on the "three-tube socket" structure.

[0043] The inventors have found through research that the existing sequential built-in three-phase separators are usually difficult to achieve extremely demanding solid phase particle (catalyst) interception rate and maintain stable and efficient separation efficiency; the existing straight-cylinder three-phase separators are difficult to avoid gas entering the three-phase separator. The area where gas enters the conventional straight-cylinder sequential three-phase separator is the liquid-solid separation area and the liquid outflow area. When the gas enters the liquid-solid separation area (i.e. Figure 1 The area between the lower end of the inner cylinder 1A and the reactor wall), the rising bubbles will disrupt the normal separation and sedimentation process of the liquid-solid separation zone, and the rising path of the bubbles is the same as the path of the liquid out of the reactor (i.e. Figure 1 The annular space between the inner and outer cylinders 2A and the reactor wall is upward), which easily causes the solid phase to flow out of the reactor with the liquid phase, deteriorating the separation effect; the expansion type three-phase separator can reduce the intrusion of bubbles to a certain extent compared with the straight type three-phase separator, but it is difficult to apply in engineering, has a complex design and a high cost. In order to solve the problems in the above-mentioned prior art, reference is made to Figure 2This embodiment realizes the "reverse order" (paper clip direction) of the material flow through the "three-tube socket" structural design, that is, the radial stroke of the first deflection and the second deflection is increased, so that the material in the central guide tube 1 is directly deflected to the annular space between the outer guide tube 2 and the reactor wall, and the radial stroke of the second deflection is effectively increased compared with the prior art, and the gas is not easy to rise in the liquid-solid separation area. In addition, since this embodiment adopts the "reverse order" material flow, even if some bubbles rise, since their rising path is opposite to the path of the liquid out of the reactor, it is not easy to cause the solid phase to flow out of the reactor with the liquid phase. Furthermore, when using a straight-cylinder reactor, this embodiment is better than the existing expansion-type reactor in preventing bubbles from rising.

[0044] Further Figure 2 、 3 As shown, the top of the central draft tube 1 is connected to the top of the outer draft tube 2 via an upper sealing baffle 4, which is located above the top of the overflow baffle 3 and is tilted. The tilted upper sealing plate design can better guide the material from the central draft tube directly into the annular space between the outer draft tube and the reactor wall.

[0045] Further Figure 2 、 3 As shown, the central draft tube 1 includes an upper straight section 11 and a lower expansion section 12. The expansion section 12 extends from the lower end of the straight section 11 toward the reactor wall. Therefore, even if some upward bubbles reach the liquid-solid separation zone, since their linear upward path is interrupted, it is difficult for the bubbles to continue upward and affect the liquid-solid separation.

[0046] The inventors further studied and found that the existing "sequential type" three-phase separator (reference Figure 1 The liquid outlet size of the reactor is not matched to the annular gap volume formed between the outer ring and the reactor wall. The area below the outlet and the annular area are the main outflow areas. The fluid flow in the area farther from the outlet is almost steady and the outflow from the annular gap is uneven. To solve the problem of uneven outflow from the annular gap, in this embodiment, the liquid phase material after the third deflection is discharged to the liquid outlet pipe 7 through the diversion buffer unit. For details, see Figures 2 to 4The flow guide buffer unit includes a curved baffle 5 and a flow guide buffer baffle 6. Among them, the curved baffle 5 extends downward from the inner wall of the outer guide tube 2, which is used to alleviate the excessive suction of the liquid phase material after the third deflection; the flow guide buffer baffle 6 is arranged at the bottom of the annular space between the outer guide tube 2 and the overflow deflection tube 3, and is arranged downward from the far end to the proximal end of the liquid outlet pipe 7, which is used to receive the drainage from the curved baffle 5 and uniformize the liquid flow rate in the annular space at the liquid outlet pipe. Preferably, but not restrictively, the inclination angle of the annular section of the upper end of the curved baffle 5 is 110°~120°; the inclination angle of the flow guide buffer baffle 6 is 5°~20°. The uniformity of the outflow of the annular gap is also a key factor in the stable and long-lasting performance of the three-phase separator. In this embodiment, the curved baffle 5 in the annular space between the outer guide tube 2 and the overflow deflector tube 3 and the guide buffer baffle 6 at the bottom can avoid excessive flow field distribution in the local annular gap, effectively solve the problem of uniformity of annular gap outflow, and help maintain the stability of the separation efficiency of the solid-liquid separation zone.

[0047] Further Figures 2 to 4 As shown, the bottom of the guide buffer baffle 6 is provided with an anti-deposition portion, which is integrally formed with the guide buffer baffle 6 and is a ring-shaped air-filled space 61 with a closed bottom (refer to Figure 4 ), the guide buffer baffle 6 serves as the upper cover of the annular inflation space 61 and has air holes 60 evenly opened at corresponding positions of the upper cover. By inflating the annular inflation space 61, bubbles generated at the air holes form turbulence for the liquid material on the guide buffer baffle 6.

[0048] Because the diverter and buffer baffle 6 employed in this embodiment is an inclined elliptical annular plate, the liquid at the other end of the liquid outlet pipe 7 possesses potential energy to flow toward the liquid outlet, thereby uniforming the flow rate of the liquid in the annular space at the liquid outlet. The anti-deposition portion is an annular space located below the diverter and buffer baffle 6, where bubbles are generated. Gas enters the annular space 61 through the inflation port 62. Once filled with gas, it can pass through a one-way gas control valve (not shown) and enter the liquid outflow area (i.e., the inclined surface of the diverter and buffer baffle 6). The bubbles generated thereby increase the turbulence of the liquid at the diverter and buffer baffle, thereby preventing coking.

[0049] Further Figure 2 、 3 As shown, an exhaust pipe 8 is provided above the third deflection position and at the connection between the upper sealing baffle 4 and the central guide tube 1. The exhaust pipes 8 are multiple and arranged in a circular array. The outlet of the exhaust pipe 8 is located above the reactor liquid level (reference Figure 5 The arrangement of the exhaust pipe array can prevent gas from mixing into the overflow area through the catalyst discharge port (i.e., the outlet of the solid catalyst particles after liquid-solid separation) and causing cavities. Example 2

[0050] like Figure 5、 6 As shown, this embodiment provides an ebullated bed reactor 100, in which the three-phase separator of Example 1 is arranged, so that the same technical effect as Example 1 can be achieved. Specifically, the reactor shell 101 is a straight cylindrical structure, a gas outlet pipe 103 is arranged at the top center of the upper head of the straight cylindrical structure, and a feed port 104 is arranged at the bottom center of the lower head of the straight cylindrical structure. The three-phase separator of Example 1 is arranged in the upper space of the reactor shell 101. Further as Figure 5 、 6 As shown, a gas-liquid distributor 105 is provided in the lower space of the reactor shell 101 and below the catalyst bed A. A solid catalyst particle filling port 106 is provided at the upper end cap, and a solid catalyst particle discharge port 107 is provided at the lower end cap.

[0051] Further Figure 5 、 6 As shown, a guide portion 102 is provided at a corresponding position on the lower end of the expansion section 12 of the central guide tube 1 of the three-phase separator. The guide portion 102 is an annular protrusion structure or a folded plate structure provided along the circumference of the inner wall of the reactor. The annular protrusion structure can be, for example, a trapezoidal or arched structure. Considering that such a structure needs to bear pressure under high-pressure conditions, compared with the annular protrusion structure, this embodiment Figure 5 and Figure 6 The baffle structure shown does not need to consider pressure bearing issues and is the preferred structure. Considering that bubbles will coalesce and form large bubble cavities between the baffle and the reactor wall, forming a certain gas film and liquid film contact state, this method has less wear on the catalyst particles.

[0052] The working process of the ebullated bed reactor is described in detail below by combining the material flow in the ebullated bed reactor of this embodiment:

[0053] First, the various regions of the three-phase separator installed within the fluidized bed reactor 100 are described: the central draft tube 1 constitutes the central flow-guiding area of ​​the three-phase separator; the outer draft tube 2 and the reactor wall form the liquid-solid descending area; the overflow baffle 3 and the central draft tube 1 form the overflow area; the overflow baffle 3 and the outer draft tube 2 form the liquid outflow area, which serves as the collection area for the clarified liquid product. The upper area of ​​the upper sealing baffle 4 is the first baffle area; the lower end of the overflow baffle 3 is the second baffle area; and the upper end of the overflow baffle 3 is the third overflow baffle area.

[0054] The gas-liquid mixture enters the gas-liquid distributor 105 through the feed port 104 at the bottom of the reactor, and then enters the catalyst bed A (the catalyst is solid catalyst particles), where a gas-liquid-solid three-phase reaction occurs in the lower middle portion of the reactor. After the reaction, the gas-liquid-solid three-phase mixture flows upward and enters the three-phase separation zone. The three-phase separator is divided into a central flow zone, a first deflection zone, a liquid-solid descending zone, a second deflection zone, an overflow zone, a third overflow deflection zone, and a liquid outflow zone, according to the order in which the liquid phase flows. Liquid-solid separation is primarily achieved in the lower portion of the second deflection zone. The liquid flows into the third overflow deflection zone using the "U"-shaped tube principle. After further separation in the third overflow deflection zone, it enters the liquid outflow zone and exits the reactor through liquid outflow pipe 7. Specifically, the gas-liquid-solid three-phase mixture first flows upward through the expansion section 12 of the central guide tube 1 through the central guide area. The flow area gradually decreases, and the flow rate of the mixture increases, forming a jet flow at the liquid level interface of the three-phase separator (i.e., the reactor liquid level B). The gas is separated here and discharged from the gas outlet pipe 103. The liquid and solid flow overflows the central guide tube 1 and enters the first deflection area, then flows into the liquid-solid descending area. The second deflection area performs liquid-solid separation, and the separated catalyst returns to the reaction area through the discharge port. After separation, the clarified liquid is obtained and enters the clarified liquid collection area through the second deflection area. An exhaust pipe 8 is provided at the top of the overflow area to prevent gas from mixing into the overflow area through the catalyst discharge port and causing a cavity. After the liquid passes through the curved baffle 5 and the lower guide buffer baffle 6 for flow field adjustment, it flows out of the reactor through the liquid outflow pipe 7. The anti-deposition part 61 generates a certain amount of bubbles in the liquid outflow area to prevent sludge deposition.

[0055] The foregoing descriptions of specific exemplary embodiments of the present invention are for purposes of illustration and description. These descriptions are not intended to limit the invention to the precise form disclosed, and it is apparent that many changes and variations are possible in light of the foregoing teachings. The exemplary embodiments are selected and described for the purpose of explaining the specific principles of the invention and their practical application, thereby enabling those skilled in the art to realize and utilize a variety of exemplary embodiments of the invention and various options and variations. Any simple modifications, equivalent variations, and modifications made to the exemplary embodiments described above are intended to fall within the scope of protection of the present invention.

Claims

1. A three-phase separator, arranged in an ebullated bed reactor and used for gas-liquid-solid three-phase separation, characterized in that: include: The central draft tube receives the gaseous and liquid materials and the solid catalyst particles carried upward from the bottom of the reactor, and forms the first deflection of the liquid and solid materials at the top; An outer draft tube is sleeved on the outside of the central draft tube, and the liquid and solid materials after the first deflection flow downward in the annular space between the outer draft tube and the reactor wall; The overflow deflector is sleeved between the central guide tube and the outer guide tube, and forms the separation of liquid and solid materials and the second deflection of liquid materials at the lower end of the overflow deflector; forms the third deflection of liquid materials at the upper end of the overflow deflector, and the liquid materials that have been deflected and descended for the third time are discharged from the liquid outlet pipe located at the lower part of the outer wall of the overflow deflector.

2. The three-phase separator according to claim 1, characterized in that The top end of the central guide tube is connected to the top end of the outer guide tube via an upper sealing baffle. The upper sealing baffle is located above the top end of the overflow deflector tube and is arranged obliquely.

3. The three-phase separator according to claim 1, characterized in that The central guide tube includes an upper straight tube section and a lower expansion section.

4. The three-phase separator according to claim 1, characterized in that After the third deflection, the liquid phase material is discharged to the liquid outlet pipe through the diversion buffer unit.

5. The three-phase separator according to claim 4, characterized in that The flow guide buffer unit includes: A curved baffle extending obliquely downward from the inner wall of the outer guide cylinder to alleviate excessive suction of the liquid phase material after the third deflection; The diversion buffer baffle is arranged at the bottom of the annular space between the outer guide tube and the overflow deflector tube, and is arranged downwardly from the distal end to the proximal end of the liquid outlet pipe, for receiving the drainage from the curved baffle and uniformizing the liquid flow rate in the annular space at the liquid outlet pipe.

6. The three-phase separator according to claim 5, characterized in that An anti-deposition portion is provided at the bottom of the diversion buffer baffle, which is integrally formed with the diversion buffer baffle and is an annular inflation space with a closed bottom. The diversion buffer baffle serves as the upper cover of the annular inflation space and has air holes evenly opened at corresponding positions of the upper cover. By inflating the annular inflation space, bubbles generated at the air holes form turbulence for the liquid material on the diversion buffer baffle.

7. The three-phase separator according to claim 5, characterized in that The inclination angle of the annular section of the upper end of the curved baffle is 110° to 120°; the inclination angle of the diversion buffer baffle is 5° to 20°.

8. The three-phase separator according to claim 2, characterized in that An exhaust pipe is provided above the third deflection position and at the connection between the upper sealing baffle and the central guide tube. The exhaust pipes are multiple and arranged in a ring array.

9. The three-phase separator according to claim 8, characterized in that The outlet of the exhaust pipe is located above the liquid level of the reactor.

10. A fluidized bed reactor, characterized in that: The three-phase separator according to any one of claims 1 to 9 is arranged in the ebullated bed reactor.

11. The ebullated bed reactor according to claim 10, characterized in that The reactor shell is a straight cylindrical structure, a gas outlet pipe is arranged at the top center of the upper head of the straight cylindrical structure, and a feed port is arranged at the bottom center of the lower head of the straight cylindrical structure; the three-phase separator is arranged in the upper space of the reactor shell.

12. The ebullated bed reactor according to claim 10, characterized in that A gas-liquid distributor is provided in the lower space of the reactor shell and below the catalyst bed.

13. The ebullated bed reactor according to claim 11, characterized in that A solid catalyst particle filling port is provided at the upper end cap position; a solid catalyst particle discharge port is provided at the lower end cap position.

14. The ebullated bed reactor according to claim 10, characterized in that A guide portion is provided at a corresponding position on the lower end of the expansion section of the central draft tube of the three-phase separator. The guide portion is an annular protrusion structure or a folded plate structure provided along the circumference of the inner wall of the reactor.

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