A liquid phase entrainment coupled gas phase feeding device, a slurry bed reactor and its application

Abstract

The present invention belongs to the technical field of chemical equipment. The present invention provides a liquid-phase entrainment coupled gas-phase feeding device, a slurry bed reactor and applications thereof. The liquid-phase entrainment coupled gas-phase feeding device is used to realize the coordination of gas feeding and liquid feeding. At the same time, a pulse ejector and a liquid-phase entrainer are used to realize a gas-liquid fully mixed circulation flow in the reactor, thereby increasing the effective coverage area of ​​the gas sweeping, thereby increasing the utilization efficiency of hydrogen and making the reaction conditions milder; at the same time, coking at the bottom of the slurry bed reactor is effectively prevented, thereby extending the continuous operation cycle of hydrogenation.

Description

Technical Field

[0001] The invention belongs to the technical field of chemical equipment, and in particular relates to a liquid phase entrainment coupled gas phase feeding device, a slurry bed reactor and applications thereof. Background Art

[0002] In recent years, the dependence on crude oil imports has been at a high level. Crude oil resources need to be used efficiently. The efficient conversion of heavy distillates, especially residual oil, is crucial. The processing of residual oil mainly adopts decarbonization and hydrogenation process routes. The decarbonization process routes represented by catalytic cracking, delayed coking, visbreaking, solvent deasphalting, etc. will produce a large amount of petroleum coke during the production process, with low resource utilization, poor product quality, and environmental pollution. In comparison, the hydrogenation process route is a more efficient route for the utilization of crude oil resources. The residual oil hydrogenation route includes fixed bed, ebullating bed and slurry bed, but the hydrogenation technology represented by fixed bed and ebullating bed is difficult to process low-quality heavy oil with high metal content and high residual carbon. The slurry bed residual oil hydrogenation technology can process more inferior residual oil raw materials with a high conversion rate, can achieve the maximum conversion of residual oil, and also has the advantages of simple equipment structure, low investment, and easy operation.

[0003] The feed distributor is one of the most important components of the slurry bed reactor. It determines the size and frequency of the original bubbles, directly affects the gas-liquid flow process in the slurry bed, plays a decisive role in the fluidization state, and also determines the performance of the reactor. However, most of the existing feed distributors have unreasonable structures, which will prevent the formation of small-sized bubbles and the full mixing of gas and liquid phases inside the reactor, thereby leading to problems such as reduced residue hydroprocessing conversion rate, coking of the lower head, and blockage of the feed distributor.

[0004] The patent application document with publication number CN101396647A discloses a fluid distributor, and designs a gas phase medium distributor for a three-phase slurry bed reactor, including a gas inlet pipe, a gas introduction pipe, a gas guide pipe, a porous gas distribution component and an impact bottom plate. Compared with the existing technology, the significant advantages of this technical solution are: the gas velocity is controlled by the resistance drop of the distributor, and the gas forms an internal circulation inside the reactor, which can effectively prevent the catalyst from settling, promote the uniform distribution of the catalyst in the axial direction of the reactor and improve the temperature distribution in the tower, with low energy consumption and easy to achieve large-scale. However, it cannot solve the problem of catalyst deposition at the bottom of the reactor.

[0005] The patent application document with the publication number CN104826558A proposes a slurry bed reactor for selective hydrogenation of acetylene to produce ethylene, wherein a gas distributor connected to the gas inlet is arranged below the slurry bed reactor; a plurality of groups of finger-shaped tubes are arranged above the gas distributor, which are arranged perpendicular to the horizontal plane, and each group of finger-shaped tubes includes a plurality of heat exchange tubes connected at the top, and the heat exchange tubes are spaced equally; a gas-liquid separator is arranged below the gas outlet of the slurry bed reactor, and a condenser is arranged below the gas-liquid separator. This technical solution solves the problems of large green oil generation, short catalyst cycle, and easy "temperature rise" of the reactor in the selective hydrogenation of acetylene to produce ethylene reaction in the fixed bed reactor, and the problems of catalyst loss, difficulty in dust removal, and severe wear of heat exchange components and reactors due to the violent collision between catalyst particles in the fluidized bed. However, it cannot solve the problem of catalyst blocking the pores of the gas distributor when the gas flow pressure is unstable or the gas supply is interrupted.

[0006] The patent document with patent number CN207463190U provides a gas distributor and a three-phase slurry bed reactor. The disclosed gas distributor includes an air inlet pipe, multiple gas distribution branches, multiple groups of gas distribution ring pipes and gas nozzles; one end of the gas distribution branch pipe is a blind end, and the other end is connected to the air inlet pipe. The two ends of the gas distribution ring pipe are respectively connected to two gas distribution branches: the gas distribution branch pipe and the gas distribution ring pipe are both provided with multiple exhaust holes, and the exhaust holes are connected to gas nozzles with downward openings, and the gas nozzles are respectively protruding from the outer walls of the gas distribution branch pipe and the gas distribution ring pipe. The structure is simple and reasonable, easy to install and manufacture, and effectively alleviates the problems of uneven gas distribution, catalyst deposition at the bottom of the reactor, unstable gas flow pressure or catalyst blocking the gas distributor when the gas supply is interrupted. However, the technical solution only involves gas distribution, and does not consider the liquid distributor and the coordination between liquid distribution and gas distribution, so as to further reduce the bubble size and strengthen the mixing of gas and liquid phases.

[0007] Therefore, it is necessary to develop a slurry bed reactor in which gas feed and liquid feed cooperate with each other, so that the gas-liquid mixed flow can enhance mass transfer while effectively preventing coking at the bottom of the slurry bed reactor, which is crucial for the efficient conversion and resource utilization of residual oil. Summary of the invention

[0008] In view of the above problems, the present invention provides a liquid-phase entrainment coupled gas-phase feeding device, a slurry bed reactor and its application. The gas feed and the liquid feed cooperate with each other to realize a fully mixed gas-liquid circulation in the reactor, a high hydrogen utilization rate, and a hydrogenation process that is not easy to coke.

[0009] In order to achieve the above object, the present invention adopts the following technical scheme:

[0010] A liquid phase entrainment coupled gas phase feeding device, comprising:

[0011] The gas phase module comprises a pressure-stabilizing gas cavity, a double-layer circular pipe concentrically arranged outside the pressure-stabilizing gas cavity, a gas phase branch pipe connecting the pressure-stabilizing gas cavity and the double-layer circular pipe, and a plurality of pulse ejectors evenly distributed at the bottom of the double-layer circular pipe; a gas phase inlet is opened at the top of the pressure-stabilizing gas cavity, and the pulse ejectors are used to generate pulse sweeping fluid;

[0012] The liquid phase module is arranged below the gas phase module, and includes a pressure-stabilizing liquid chamber, a plurality of liquid phase branches radially distributed on the outer side wall of the pressure-stabilizing liquid chamber, and at least one liquid phase entrainer connected to the top of the outer end of each of the liquid phase branches; a suction port for entraining surrounding liquid and bubbles generated by the pulse ejector is provided on the outer side wall of the liquid phase entrainer, and a liquid phase inlet is provided at the bottom of the pressure-stabilizing liquid chamber.

[0013] The present invention is further configured such that the double-layer circular ring pipe includes a gas phase inner ring pipe and a gas phase outer ring pipe which are arranged concentrically with the pressure-stabilizing air cavity, the inner end of the gas phase branch pipe is connected to the pressure-stabilizing air cavity, and the outer end extends outward and is connected to the gas phase inner ring pipe and the gas phase outer ring pipe in sequence.

[0014] The present invention is further configured such that the pulse jet includes an inlet portion, a main channel and a first nozzle portion which are connected in sequence, and a pair of feedback channels arranged on both sides of the main channel for periodically changing the jet direction of the first nozzle portion, the inlet and the outlet of the feedback channel are respectively connected to the inlet portion and the first nozzle portion, and the inlet portion is connected to a double-layer circular pipe.

[0015] The present invention is further configured such that the inlet portion is a tapered inlet, the first nozzle portion is an umbrella-shaped nozzle, and the spraying angle of the first nozzle portion is 100° to 150°.

[0016] The present invention is further configured such that the pulse ejector is arranged at the bottom of the gas phase inner ring tube and the gas phase outer ring tube between two adjacent gas phase branches; and the pulse ejector is inclined along the tangent direction of the double-layer circular ring pipe, and the angle between the pulse ejector and the vertical direction is 15°~25°.

[0017] The present invention is further configured such that the pulse jets have the same inclination direction, which is either clockwise or counterclockwise.

[0018] The present invention is further configured as follows: the liquid phase entrainer includes a convergent nozzle portion and a second nozzle portion connected to the convergent nozzle portion, and the small diameter end of the convergent nozzle portion extends into the second nozzle portion, and the gap between the inner end of the second nozzle portion and the large diameter section of the convergent nozzle portion forms the entrainment port, and the entrainment port is close to the outlet of the convergent nozzle portion; after the liquid phase enters the convergent nozzle portion, its speed increases, and a local negative pressure is formed at the outlet of the convergent nozzle portion, so that the liquid and bubbles around the entrainment port are entrained into the liquid phase entrainer through the entrainment port.

[0019] The present invention provides a slurry bed reactor, comprising a slurry bed reactor body and a feeding device arranged inside the slurry bed reactor body, wherein the feeding device adopts the above-mentioned liquid phase entrainment coupled gas phase feeding device.

[0020] The present invention is further configured such that the liquid phase entrainment coupled gas phase feeding device is arranged at the bottom of the slurry bed reactor, and the distance between the pressure-stabilizing gas cavity and the bottom surface of the lower head of the slurry bed reactor is 0.2h~0.6h, where h is the total height of the lower head based on the bottom surface of the lower head.

[0021] The present invention is further configured such that the pressure-stabilizing air cavity and the pressure-stabilizing liquid cavity are coaxially arranged, and the spacing between the pressure-stabilizing air cavity and the pressure-stabilizing liquid cavity is 0.1h~0.4h.

[0022] The present invention is further configured such that the inner diameter of the slurry bed reactor body is D, and the vertical spacing between the liquid phase entrainer and the pulse ejector is 0.1D-0.3D. Furthermore, the spacing between the liquid phase entrainer and the pulse ejector is controlled to be 50mm-500mm.

[0023] The present invention is further configured as follows: the inner diameter of the slurry bed reactor body is D, the length of the gas phase branch pipe is 0.3-0.4 times the diameter D of the slurry bed reactor, the diameter of the gas phase inner ring pipe is 0.3D-0.5D, and the diameter of the gas phase outer ring pipe is 0.6D-0.8D; the length of the liquid phase branch pipe is 0.2D~0.4D.

[0024] The present invention also provides an application of a slurry bed reactor for hydrogenation reaction, wherein hydrogen is transported to the gas phase module as a gas phase, and the reaction liquid is transported to the liquid phase module as a liquid phase.

[0025] Compared with the prior art, the present invention has the following beneficial technical effects:

[0026] (1) The liquid-phase entrainment coupled gas-phase feeding device provided by the present invention integrates a gas distributor and a liquid distributor, and utilizes liquid-phase entrainment coupled gas-phase pulsating sweeping feeding mode to make the gas feed and the liquid feed cooperate with each other to realize a gas-liquid fully mixed circulation flow in the reactor, with high hydrogen utilization rate, milder reaction conditions, and a hydrogenation process that is not prone to coking.

[0027] (2) The present invention adopts a pulse ejector, which utilizes flow shear and vortex effects to break hydrogen into small-sized bubbles. The gas phase pulse sweeping position will change with time, forming different gas phase rising positions in the slurry bed reactor, promoting gas-liquid full mixed circulation and enhancing reaction mass transfer. At the same time, the pulse ejector nozzle angle is 100°~150°. Compared with the traditional gas phase feeder, the effective coverage area of ​​gas sweeping can be increased by 50%-150%, which can significantly reduce the number of gas phase feeders installed, thereby reducing the blockage rate of the feed hole;

[0028] (3) The liquid phase entrainer used in the present invention can increase the speed by using a tapered nozzle and form a local negative pressure at the nozzle outlet. Under the action of the entrainment structure, the surrounding liquid and the bubbles generated by the pulse ejector are entrained into the liquid phase entrainer and broken under the shearing action of the high-speed liquid phase to form a micro-scale bubble group with a bubble size of 0.2mm-1mm. The gas-liquid mixed flow can effectively prevent coking at the bottom of the slurry bed reactor while enhancing mass transfer. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] Figure 1 This is a schematic diagram of the structure of the slurry bed reactor described in the present invention.

[0030] Figure 2 This is a schematic diagram of the gas phase module structure of the present invention.

[0031] Figure 3 This is a bottom view of the gas phase module of the present invention.

[0032] Figure 4 This is a schematic diagram of the pulse jet device described in the present invention.

[0033] Figure 5 This is a comparison diagram between the pulse ejector of the present invention and a conventional gas phase feeder, wherein the left side is the pulse ejector and the right side is the conventional gas phase feeder.

[0034] Figure 6 This is a schematic diagram of the liquid phase module structure of the present invention.

[0035] Figure 7 This is a top view of the liquid phase module of the present invention.

[0036] Figure 8 This is a schematic diagram of the liquid phase entrainer of the present invention.

[0037] Among them, 1. slurry bed reactor body, 2. gas phase main pipe, 3. liquid phase main pipe; 100. gas phase module, 110. pressure-stabilizing gas cavity, 120. double-layer circular ring pipe, 121. gas phase inner ring pipe, 122. gas phase outer ring pipe; 130. gas phase branch pipe, 140. pulse ejector, 141. inlet part, 142. main channel, 143. first nozzle part, 144. feedback channel, 200. liquid phase module, 210. pressure-stabilizing liquid cavity, 220. liquid phase branch pipe, 230. liquid phase entrainer, 231. tapered nozzle part, 232. second nozzle part, 233. entrainment port. DETAILED DESCRIPTION

[0038] The technical solution of the present invention will be clearly and completely described below in conjunction with specific embodiments. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments.

[0039] Example 1

[0040] refer to Figure 1 , an embodiment of the present invention provides a slurry bed reactor, the slurry bed reactor comprises a slurry bed reactor body 1 and a liquid-phase entrainment-coupled gas-phase feeding device, the liquid-phase entrainment-coupled gas-phase feeding device is arranged inside the slurry bed reactor body 1, and is used to transport gas and liquid phases into the slurry bed reactor;

[0041] The liquid phase entrainment coupled gas phase feeding device comprises:

[0042] The gas phase module 100 includes a pressure-stabilizing gas cavity 110, a double-layer circular pipe 120 concentrically arranged outside the pressure-stabilizing gas cavity 110, a gas phase branch pipe 130 connecting the pressure-stabilizing gas cavity 110 and the double-layer circular pipe 120, and a plurality of pulse ejectors 140 evenly distributed at the bottom of the double-layer circular pipe 120; the pulse ejectors 140 are used to generate pulse sweeping fluid, and a gas phase inlet (not shown in the figure) is opened at the top of the pressure-stabilizing gas cavity 110, through which the gas phase material is input into the gas phase module 100 and then ejected through the pulse ejectors 140;

[0043] The liquid phase module 200 is arranged below the gas phase module 100, and includes a pressure-stabilizing liquid chamber 210, a plurality of liquid phase branches 220 uniformly and radially distributed on the outer wall of the pressure-stabilizing liquid chamber 210, and at least one liquid phase entrainer 230 arranged at the top of the outer end of each liquid phase branch pipe 220; the bottom inlet of the liquid phase entrainer 230 is connected to the liquid phase branch pipe 220, and the outer wall of the liquid phase entrainer 230 is provided with an entrainment port for entraining the liquid around it and the bubbles generated by the pulse ejector 140; the bottom of the pressure-stabilizing liquid chamber 210 is provided with a liquid phase inlet (not shown in the figure), through which the liquid phase material is input into the gas phase module 100 and then discharged through the liquid phase entrainer 230.

[0044] In the present invention, the gas phase inlet is connected to a gas phase main pipe 2, and the gas phase main pipe 2 passes through the outer wall of the slurry bed reactor body 1 to be connected to the external gas source. The liquid phase inlet is connected to a liquid phase main pipe 3, and the liquid phase main pipe 3 passes through the bottom of the slurry bed reactor body 1 to be connected to the external liquid phase source.

[0045] In the present invention, the double-layer circular pipe 120 includes a concentrically arranged gas phase inner ring pipe 121 and a gas phase outer ring pipe 122, the inner end of the gas phase branch pipe 130 is connected to the outer side wall of the pressure-stabilizing gas cavity 110, and the outer end extends outward and is sequentially connected to the gas phase inner ring pipe 121 and the gas phase outer ring pipe 122. The gas entering the pressure-stabilizing gas cavity 110 is transported to the gas phase inner ring pipe 121 and the gas phase outer ring pipe 122 through the gas phase branch pipe 130.

[0046] like Figure 2 As shown, in the present invention, the pulse ejector 140 is installed at the bottom of the gas phase inner ring tube 121 and the gas phase outer ring tube 122 along the tangent direction of the double-layer circular pipe 120 where it is located, and the inclination direction is consistent, both of which are inclined in the clockwise direction or counterclockwise direction; the angle between the pulse ejector 140 and the vertical direction is 15°~25°, so that the gas injection direction and the liquid injection direction of the liquid phase entrainer 230 installed vertically below are misaligned.

[0047] like Figure 3 As shown, in the present invention, the pulse ejectors 140 are evenly distributed on the gas phase inner ring pipe 121 and the gas phase outer ring pipe 122 between two adjacent gas phase branches 130. This avoids installing the pulse ejectors 140 at the connection between the gas phase inner ring pipe 121, the gas phase outer ring pipe 122 and the gas phase branch pipe 130.

[0048] refer to Figure 4 and Figure 5The pulse jet device 140 includes an inlet portion 141, a main channel 142, and a first nozzle portion 143 which are connected in sequence from top to bottom, and a pair of feedback channels 144 arranged on both sides of the main channel 142 for periodically changing the jet direction of the first nozzle portion; the inlet portion 141 is connected to the double-layer circular ring pipe 120, and the inlet end and the outlet end of the feedback channel 144 are respectively connected to the inlet portion 141 and the first nozzle portion 143; the inlet portion 141 is a tapered inlet, the first nozzle portion 143 is an umbrella-shaped outlet, and the nozzle angle of the first nozzle portion 143 is 100°~150°; the nozzle angle of the first nozzle portion 143 is preferably 120°.

[0049] After the gas phase enters the pulse ejector from the double-layer circular pipe 120 through the inlet 141, the gas velocity increases significantly, and most of the gas will flow through the main channel 142 with greater kinetic energy and be ejected through the first nozzle 143; a small part of the gas enters the feedback channel and intermittently flows back to the main channel again, and causes instantaneous disturbances and changes to the airflow in the main channel. This disturbance and change will occur intermittently and periodically, affecting the position of the small-sized bubbles ejected from the nozzle, forming a stable pulsating sweep frequency. Since the gas phase pulse sweeping position of the pulse ejector will change with time, different gas phase rising positions will be formed in the slurry bed reactor 1, promoting the full mixed circulation of gas and liquid and strengthening the reaction mass transfer. However, since the traditional gas phase feeder does not have a feedback channel designed inside, the gas sweeping range it ejects is relatively small. Compared with the traditional gas phase feeder, the effective coverage area of ​​the gas sweep of the pulse ejector of the present invention can be increased by 50%-150%.

[0050] refer to Figure 6~Figure 8 The liquid phase entrainer 230 includes a tapered nozzle portion 231 and a second nozzle portion 232 installed on the tapered nozzle portion 231, the small diameter end of the tapered nozzle portion 231 extends into the second nozzle portion 232, the gap between the inner end of the second nozzle portion 232 close to the tapered nozzle portion 231 and the large diameter end of the tapered nozzle portion 231 forms the entrainment port 233, and the entrainment port 233 is close to the outlet of the tapered nozzle portion 231; the second nozzle portion 232 can be fixed to the outer wall of the tapered nozzle portion by a bracket, and the fixing method can be a fixing part or welding or other commonly used fixing methods in the field. After the liquid phase passes through the tapered nozzle portion 231 and enters the liquid phase entrainer 230, its speed increases, forming a local negative pressure at the outlet of the tapered nozzle portion 231, and the liquid and bubbles around the entrainment port 233 are entrained into the liquid phase entrainer 230, and ejected through the top of the second nozzle portion 232; under the shearing action of the high-speed liquid phase, a micro-scale bubble group with a bubble size of 0.2mm-1mm is formed, and the gas-liquid mixed flow can effectively prevent coking at the bottom of the slurry bed reactor while enhancing mass transfer.

[0051] In the present invention, the pulse ejector 140 and the gas phase inner ring pipe 121 and the gas phase outer ring pipe 122, as well as the liquid phase entrainer 230 and the liquid phase branch pipe 220 are all connected via flanges.

[0052] Furthermore, in the present invention, the liquid-phase entrainment-coupled gas-phase feeding device is arranged at the bottom of the slurry bed reactor, and the distance between the pressure-stabilizing gas chamber 110 and the bottom surface of the lower head of the slurry bed reactor is 0.2h~0.6h, where h is the total height of the lower head based on the bottom surface of the lower head.

[0053] In the present invention, the pressure-stabilizing air cavity 110 and the pressure-stabilizing liquid cavity 210 are coaxially arranged, and the distance between the pressure-stabilizing air cavity and the pressure-stabilizing liquid cavity is 0.1h~0.4h.

[0054] According to the technical solution provided by the present invention, those skilled in the art can adjust the spacing between the pulse ejector 140 and the liquid phase entrainer 230 according to actual needs, so that the liquid phase entrainer can better entrain the bubbles generated by the pulse ejector 140. Preferably, in the present invention, the inner diameter of the slurry bed reactor is D, and the vertical spacing between the liquid phase entrainer 230 and the pulse ejector 140 is 0.1D~0.3D; this setting can effectively sweep the small-sized bubbles ejected by the pulse ejector to the bottom surface of the lower head as much as possible to prevent the bottom surface of the lower head from coking, and after further breaking after colliding with the bottom surface of the lower head, most of them are entrained by the liquid phase entrainer for secondary shearing to form micro-scale bubbles.

[0055] In the present invention, the diameter of the slurry bed reactor body 1 is D, the length of the gas phase branch pipe 130 is 0.3-0.4 times the diameter D of the slurry bed reactor, the diameter of the gas phase inner ring pipe 121 is 0.3D-0.5D, and the diameter of the gas phase outer ring pipe 122 is 0.6D-0.8D; the length of the liquid phase branch pipe 220 is 0.2D~0.4D.

[0056] The working process of the liquid-phase entrainment coupled gas-phase feeding device of the present invention is as follows: the gas phase and the liquid phase are transported to the gas phase module 100 and the liquid phase module 200 respectively through the gas phase main pipe 2 and the liquid phase main pipe 3; the gas phase first enters the pressure-stabilizing gas cavity 110 to stabilize the pressure, and then the hydrogen is evenly distributed to the gas phase inner ring pipe 121 and the gas phase outer ring pipe 122 through the gas phase branch pipe 130, and pulse sweeping is generated when passing through the pulse ejector, and the bubble size generated is 1mm~3mm; the gas phase pulse sweeping position will change with time, forming different gas phase rising positions in the slurry bed reactor, promoting gas-liquid full mixed circulation, and strengthening reaction mass transfer;

[0057] The liquid phase first enters the pressure-stabilizing liquid chamber 210 to stabilize the pressure, and then is distributed to each liquid phase branch pipe 220, and enters the liquid phase entrainer 230 along the liquid phase branch pipe 220. The liquid phase increases in speed after passing through the tapered nozzle of the liquid phase entrainer, and forms a local negative pressure at the nozzle outlet. Under the action of the entrainment structure, the surrounding liquid and the bubbles generated by the pulse ejector are entrained into the liquid phase entrainer, and are broken under the shearing action of the high-speed liquid phase to form a micro-scale bubble group with a bubble size of 0.2mm-1mm. The gas-liquid mixed flow can effectively prevent coking at the bottom of the slurry bed reactor while enhancing mass transfer.

[0058] Example 2

[0059] The liquid phase entrainment coupled gas phase feeding device and slurry bed reactor described in Example 1 were used, and the average bubble diameter, gas phase average specific surface area and average gas holdup were compared under the same conditions when the interval d between the pulse ejector 140 and the liquid phase entrainer 230 was different. The average bubble diameter, average bubble specific surface area and average gas holdup were screened as the test standard. Under the same conditions, the smaller the average bubble diameter, the larger the average bubble specific surface area and the average gas holdup, the better the gas-liquid mixing and mass transfer of the reactor. D is the diameter of the slurry bed reactor. The results are shown in Table 1.

[0060] Table 1 Test results at different distances d between the liquid phase entrainer and the pulse ejector

[0061]

[0062] According to the experimental process and test results, when d=0.4D, the distance between the two is large, and most of the small-sized bubbles ejected by the pulse ejector 140 cannot be entrained by the liquid phase entrainer 230 for secondary shearing to form micro-scale bubbles, resulting in the largest average bubble diameter, the smallest average specific surface area and the smallest average gas content. When d=0.05D, the distance between the two is small, and part of the bubbles ejected from the nozzle of the pulse ejector 140 will be directly entrained by the liquid phase entrainer, and the other part will be swept onto the liquid phase branch pipe, which cannot play the role of sweeping the bottom surface of the lower head to prevent coking, and the bubble diameter is moderate, the specific surface area is the smallest, and the installation and disassembly are more difficult; when d=0.20D, the small-sized bubbles ejected by the pulse ejector are effectively swept onto the bottom surface of the lower head to prevent coking, and after further breaking after colliding with the bottom surface of the lower head, most of them are entrained by the liquid phase entrainer for secondary shearing to form micro-scale bubbles, resulting in the smallest average bubble diameter, the largest average specific surface area and the largest average gas content. Therefore, designing a suitable distance between the liquid phase entrainer and the pulse ejector plays an important role in improving the effect of the device of the present invention.

[0063] Application Example 1

[0064] The properties of the residual oil raw materials of a petrochemical plant are shown in Table 2 below:

[0065] Table 2 Residue oil raw material properties:

[0066]

[0067] In this application example, the slurry bed reactor described in Example 1 is used to hydrotreat the residual oil, hydrogen is transported through the gas phase main pipe, the nozzle angle of the pulse ejector is 120°, the pulsation frequency of the pulse ejector is 0.005-0.01s / time, and the distance between the pulse ejector and the liquid phase entrainer is 0.2D. The reaction pressure, hydrogen-to-oil volume ratio and residual oil conversion rate inside the slurry bed reactor are shown in Table 3.

[0068] Application Comparative Example 1

[0069] Compared with Application Example 1, the difference is that in this comparative application example, the slurry bed reactor uses the internal components of the conventional bubbling reactor in the art, and other operating conditions are the same. The pressure, hydrogen-to-oil volume ratio and residue oil conversion rate required for the hydrogenation reaction are specifically shown in Table 3 below.

[0070] Table 3 Performance parameter comparison table of application example 1 and application comparative example 1

[0071]

[0072] It can be seen from the results in Table 3 that, under almost the same operating conditions, the liquid-phase entrainment coupled gas-phase feeding device designed by the present invention requires a significantly lower reaction pressure and hydrogen-to-oil volume ratio than those of Application Comparative Example 1, and a significantly higher residual oil conversion rate than that of Application Comparative Example 1. Moreover, after long-term operation of the reactor, it is found that the coking condition of Application Example 1 is better than that of Application Comparative Example 1.

[0073] In summary, the slurry bed reactor with a liquid-phase entrainment coupled gas-phase pulsating sweeping feeding method proposed in the present invention is applied in actual production, which can realize a fully mixed gas-liquid circulation in the slurry bed reactor, enhance flow mass transfer, improve hydrogen utilization, and reduce the hydrogen-to-oil ratio; at the same time, it can effectively inhibit coking and extend the continuous operation cycle of hydrogenation.

[0074] The specific embodiments of the present invention are described in detail above, but they are only examples, and the present invention is not limited to the specific embodiments described above. For those skilled in the art, any equivalent modification and substitution of the practical is also within the scope of the present invention. Therefore, the equalization transformation and modification made without departing from the spirit and scope of the present invention should be included in the scope of the present invention.

Claims

1. A liquid phase entrainment coupled gas phase feeding device for a slurry bed reactor, characterized in that: include: A gas phase module, comprising a pressure-stabilizing air cavity, a double-layer circular ring pipe concentrically arranged outside the pressure-stabilizing air cavity, a gas phase branch pipe connecting the pressure-stabilizing air cavity and the double-layer circular ring pipe, and a plurality of pulse ejectors evenly distributed at the bottom of the double-layer circular ring pipe; a gas phase inlet is provided at the top of the pressure-stabilizing air cavity, and the pulse ejector is used to generate a pulse sweeping fluid; the pulse ejector comprises an inlet portion, a main flow channel and a first nozzle portion connected in sequence, and a pair of feedback channels arranged on both sides of the main flow channel for periodically changing the jet direction of the first nozzle portion, the inlet and the outlet of the feedback channel are respectively connected to the inlet portion and the first nozzle portion, and the inlet portion is connected to the double-layer circular ring pipe; A liquid phase module is arranged below the gas phase module, comprising a pressure-stabilizing liquid chamber, a plurality of liquid phase branches radially distributed on the outer side wall of the pressure-stabilizing liquid chamber, and at least one liquid phase entrainer connected to the top of the outer side end of each of the liquid phase branches; a suction port for entraining surrounding liquid and bubbles generated by the pulse ejector is provided on the outer side wall of the liquid phase entrainer, and a liquid phase inlet is provided at the bottom of the pressure-stabilizing liquid chamber; the liquid phase entrainer comprises a tapered nozzle portion and a second nozzle portion connected to the tapered nozzle portion, the small diameter end of the tapered nozzle portion extends into the second nozzle portion, the suction port is formed by a gap between the inner side end of the second nozzle portion and the large diameter section of the tapered nozzle portion, and the suction port is close to the outlet of the tapered nozzle portion; The inner diameter of the slurry bed reactor body is D, and the vertical distance between the liquid phase entrainer and the pulse ejector is 0.1D to 0.3D.

2. The liquid phase entrainment coupled gas phase feeding device according to claim 1, characterized in that: The double-layer circular ring pipeline includes a concentrically arranged gas phase inner ring pipe and a gas phase outer ring pipe, the inner end of the gas phase branch pipe is connected to the pressure-stabilizing gas cavity, and the outer end extends outward and is connected to the gas phase inner ring pipe and the gas phase outer ring pipe in sequence.

3. The liquid phase entrainment coupled gas phase feeding device according to claim 1, characterized in that: The first nozzle portion is an umbrella-shaped nozzle, and the spraying angle of the first nozzle portion is 100° to 150°.

4. The liquid phase entrainment coupled gas phase feeding device according to claim 2, characterized in that: The pulse ejector is arranged at the bottom of the gas phase inner ring tube and the gas phase outer ring tube between two adjacent gas phase branches; and the pulse ejector is inclined along the tangent direction of the double-layer circular ring pipe, and the angle between the pulse ejector and the vertical direction is 15° to 25°.

5. A slurry bed reactor, characterized in that: It comprises a slurry bed reactor body and a feeding device arranged inside the slurry bed reactor body, wherein the feeding device adopts the liquid phase entrainment coupled gas phase feeding device as claimed in any one of claims 1 to 4.

6. The slurry bed reactor according to claim 5, characterized in that: The liquid phase entrainment coupled gas phase feeding device is arranged at the bottom of the slurry bed reactor, and the distance between the pressure stabilizing gas cavity and the bottom surface of the lower head of the slurry bed reactor is 0.2h-0.6h, where h is the total height of the lower head when the bottom surface of the lower head is taken as the reference; The pressure-stabilizing air cavity and the pressure-stabilizing liquid cavity are coaxially arranged, and the distance between the pressure-stabilizing air cavity and the pressure-stabilizing liquid cavity is 0.1h-0.4h.

7. The slurry bed reactor according to claim 5, characterized in that: The inner diameter of the slurry bed reactor body is D, and the vertical distance between the liquid phase entrainer and the pulse ejector is 0.1D to 0.3D; The double-layer circular ring pipeline includes a concentrically arranged gas phase inner ring tube and a gas phase outer ring tube, the inner end of the gas phase branch pipe is connected to the pressure-stabilizing gas cavity, and the outer end extends outward and is connected to the gas phase inner ring tube and the gas phase outer ring tube in sequence; the length of the gas phase branch pipe is 0.3-0.4 times the diameter D of the slurry bed reactor, the diameter of the gas phase inner ring tube is 0.3D-0.5D, and the diameter of the gas phase outer ring tube is 0.6D-0.8D; the length of the liquid phase branch pipe is 0.2D~0.4D.

8. An application of a slurry bed reactor, characterized in that: The slurry bed reactor according to any one of claims 5 to 7 is used for hydrogenation reaction, hydrogen is transported to the gas phase module as a gas phase, and the reaction liquid is transported to the liquid phase module as a liquid phase.

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