CN217042506U - Up-going residual oil hydrogenation reactor with fractal bubble size - Google Patents
Up-going residual oil hydrogenation reactor with fractal bubble size Download PDFInfo
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- CN217042506U CN217042506U CN202123367784.6U CN202123367784U CN217042506U CN 217042506 U CN217042506 U CN 217042506U CN 202123367784 U CN202123367784 U CN 202123367784U CN 217042506 U CN217042506 U CN 217042506U
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Abstract
The utility model provides an upstroke type residual oil hydrogenation reactor with fractal bubble scale, which comprises an outer cylinder, wherein a bubble distribution clapboard is arranged in the outer cylinder, a hydrogenation catalyst is filled above the bubble distribution clapboard, and a first mixing cavity is arranged below the bubble distribution clapboard; a bubbler and a fractal bubble generator are arranged at the bottom end of the outer cylinder in the first mixing cavity; the bottom end of the outer barrel is provided with a first gas-phase inlet, a second gas-phase inlet and a liquid-phase inlet, the first gas-phase inlet and the liquid-phase inlet are respectively communicated with a gas-liquid-phase inlet of the fractal bubble generator, and the second gas-phase inlet is communicated with the bubbler; the top end of the outer barrel is provided with a discharge hole. The utility model discloses a fractal bubble generator and bubbler combination hydrogenation produce fractal bubble and big bubble and mix and get into the catalyst bed, improve gas-liquid mass transfer rate, improve the reaction effect, slowed down the coking and blockked up, the too big scheduling problem of pressure drop, effectively prolong residual oil hydrogenation reaction period.
Description
Technical Field
The utility model belongs to the technical field of residual oil hydrogenation, concretely relates to upstroke residual oil hydrogenation ware of bubble yardstick fractal.
Background
Petroleum is the most widely used energy source in the world at present, and residue hydrogenation mainly comprising atmospheric residue and vacuum residue is one of the important ways for lightening heavy oil. The residue oil hydrogenation technology refers to a reaction process of petroleum fractions and hydrogen under the action of a catalyst, and is an important means for refining and modifying petroleum products and processing heavy oil. The purpose of oil product modification is to remove nitrogen, oxygen, sulfur and other heteroatoms and metal impurities in the oil product, or to hydrogenate and saturate some aromatic hydrocarbons and olefins, thereby improving the service performance of the oil product.
The residual oil hydrogenation reaction technology currently comprises reactor forms such as a fixed bed, a moving bed, a fluidized bed, a suspended bed, a slurry bed and the like, wherein the latter four technologies have the problems of easy abrasion of a catalyst, difficult control of gas retention time and the like. The main technical advantages of stable reaction process, simple structure and long service life of the catalyst in the fixed bed reactor are rapidly developed, and become the most mature mainstream technology of residual oil hydrogenation. Along with the stricter environmental protection laws and the stricter petroleum quality requirements in recent years, more and more oil refining enterprises select the fixed bed hydrogenation and residual oil catalytic cracking combined process, so that the mass production of high-quality gasoline, kerosene and diesel oil is realized, remarkable economic and social benefits are obtained, and the industrial prospect is good.
A fixed bed residual oil hydrogenation reactor is a gas-liquid-solid three-phase reactor, and the problems of overlarge pressure drop and insufficient hydrogen mass transfer exist in the conventional hydrogenation reactor. The smaller the bubbles in the reactor are, the larger the specific surface area of the bubbles is, and the larger the gas-liquid contact surface of liquid in unit volume is, so that the gas-liquid-solid mass transfer is facilitated; meanwhile, the smaller the bubble, the slower the rising speed of the bubble, and the longer the residence time of the small bubble in the reactor with the same height, the more beneficial to gas-liquid-solid mass transfer. In addition, from the perspective of bubble coalescence, the smaller the bubble, the lower the bubble coalescence probability in the bubble rising process, so that the smaller bubble size can be further maintained, which is favorable for mass transfer. In the existing fixed bed residual oil hydrogenation technology, hydrogen usually enters a bed layer in a bubbling mode, the diameter of hydrogen bubbles is larger, the average diameter is more than 10mm, and the hydrogen cannot effectively cover gaps among catalyst particles after entering a catalyst particle bed layer, so that the gas-liquid-solid three-phase contact area is small, the hydrogen cannot be rapidly supplemented after participating in reaction consumption, the coking rate is high due to local hydrogen deficiency, the secondary oil is difficult to process, the device has the problems of high operation severity requirement, poor raw material adaptability, short operation period and the like, and the processing capacity and level of the device are limited; in addition, the operating temperature of the existing reactor is high, which affects the service life of the catalyst. The hydrogenation of residual oil in a fixed bed is continuously consumed along with the hydrogen in the reaction, in order to ensure the hydrogen supplement rate, a high-efficiency mass transfer method is needed to accelerate the mass transfer rate of the hydrogen in a reactor, and meanwhile, in order to solve the problems of uneven temperature distribution and overlarge pressure drop of the fixed bed, a gas-liquid phase is needed to be filled in gaps of catalyst particles, and the hydrogen is uniformly distributed in a catalyst bed layer.
CN201644076U provides a liquid phase hydrogenation ware, sets up the blender between the catalyst bed in the reactor, the blender is equipped with dissolves hydrogen mixture export and dissolve hydrogen mixture export and soak in next catalyst bed liquid, and this blender can increase the alternate area of contact of gas-liquid effectively, and simple structure makes hydrogen dissolve in the miscella, improves the efficiency of hydrogenation. However, the reactor does not improve the gas-liquid reaction efficiency on the basis of the bubble scale, the turbulent kinetic energy is low, and the hydrogen is easy to diffuse upwards and escape, so that the utilization rate of the hydrogen is reduced.
SUMMERY OF THE UTILITY MODEL
The utility model aims at overcoming the not enough of prior art, improving the gas-liquid mass transfer rate in the fixed bed residual oil hydrogenation ware, improving reactor reaction effect, extension hydrogenation's reaction cycle provides an upstroke residual oil hydrogenation ware of bubble yardstick fractal, utilizes fractal bubble generator and bubbler combination hydrogenation.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
an upstroke type residual oil hydrogenation reactor with fractal bubble size comprises an outer cylinder, wherein a bubble distribution partition plate is arranged in the outer cylinder, the periphery of the bubble distribution partition plate is connected with the inner wall of the outer cylinder, a hydrogenation catalyst is filled above the bubble distribution partition plate, and a first mixing cavity is arranged below the bubble distribution partition plate; a bubbler and a fractal bubble generator are arranged at the bottom end of the outer barrel in the first mixing cavity; the bottom end of the outer barrel is provided with a first gas-phase inlet, a second gas-phase inlet and a liquid-phase inlet, the first gas-phase inlet and the liquid-phase inlet are respectively communicated with a gas-liquid-phase inlet of the fractal bubble generator, and the second gas-phase inlet is communicated with the bubbler; and a discharge hole is formed in the top end of the outer barrel.
The utility model discloses further set up to, the bubbler is annular bubbler, fractal bubble generator is located the centre ring department of bubbler just is located the top of bubbler for cut the gaseous phase through liquid phase whirl and produce the fractal bubble.
The utility model discloses further set up as, fractal bubble generator's upper end distance the bubble distribution baffle is 1-4 m.
The utility model discloses further set up to, the bubbler is equipped with trompil drum bubble up, the drum bubble distributes along annular bubbler equidistance, and the aperture is 2-7 mm.
The utility model discloses further set up to, fractal bubble generator's lateral wall is equipped with liquid phase tangential import, and the bottom is equipped with gaseous phase axial import, be equipped with the intercommunication in the fractal bubble generator the second hybrid chamber of liquid phase tangential import and gaseous phase axial import, gaseous phase axial import with be equipped with the throat of admitting air between the second hybrid chamber, the upper end of second hybrid chamber is equipped with the throat export, throat exit linkage spiral shear blade.
The utility model discloses further set up as, the height to diameter ratio of second hybrid chamber is (2-4): 1; the ratio of the diameter of the air inlet throat to the diameter of the second mixing chamber is 0.05-0.3.
The utility model is further arranged in such a way that the helix angle alpha of the helical shearing blade is 20-50 degrees.
The utility model discloses further set up to, the bubble distributes the baffle and is equipped with a plurality of apertures, the aperture of aperture is 2-4 mm.
The utility model discloses further set up to, the distribution form of aperture is along baffle center to outer fringe equidistance circumference distribution.
Compared with the prior art, the utility model discloses following beneficial effect has:
the upstroke residual oil hydrogenation reactor adopts the traditional bubbling and fractal bubble combined hydrogenation, in a catalyst bed layer, micro bubbles distributed in fractal bubbles are fully mixed with residual oil, gaps among catalyst particles are filled, the residence time of the micro bubbles is long, the gas content of hydrogen in the residual oil hydrogenation reactor is improved, the gas-liquid contact area is increased, and meanwhile, hydrogen consumed by reaction can be quickly supplemented; large bubbles generated by bubbling provide a turbulent effect, so that the liquid-phase mass transfer coefficient of the hydrogenation reaction is greatly improved, and the conversion rate of the residual oil hydrogenation reaction is improved; the gas-liquid phase is uniformly distributed in the height direction and the cross section direction of the catalyst bed layer, thereby inhibiting coking, reducing pressure drop, improving the utilization rate of the catalyst and hydrogen, prolonging the operation period of residual oil hydrogenation and improving economic benefit.
Drawings
FIG. 1 is a schematic structural diagram of an upstroke residual oil hydrogenation reactor related to the present invention;
fig. 2 is a schematic structural diagram of a fractal bubble generator according to the present invention;
fig. 3 is a schematic structural diagram of a spiral shearing blade of the fractal bubble generator according to the present invention;
FIGS. 4A and 4B are cross-sectional views taken along plane C-C of FIG. 1;
FIG. 5 is a schematic representation of the distribution and fullness of bubbles in the catalyst void space generated by conventional bubbling, shown schematically in the cross-section of a maximum of non-spherical catalyst particles;
FIG. 6 is a schematic representation of the distribution and fullness of bubbles in a catalyst void created by a combination of conventional bubbling and fractal bubbles, shown schematically in cross-section with the largest non-spherical catalyst particle;
the device comprises a 1-up residual oil hydrogenation reactor, 6-large bubbles, 7-fine bubbles, 8-catalyst particles, 11-outer cylinders, 12-bubble distribution partition plates, 13-first mixing cavities, 14-bubblers, 15-fractal bubble generators, 16-first gas phase inlets, 17-second gas phase inlets, 18-liquid phase inlets, 19-discharge ports, 121-small holes, 151-liquid phase tangential inlets, 152-gas phase axial inlets, 153-second mixing cavities, 154-gas inlet throats, 155-throat outlets and 156-spiral shearing blades.
Detailed Description
The technical solution of the present invention is further explained by the following embodiments with reference to the drawings.
The utility model provides an upstroke type residual oil hydrogenation reactor with a fractal bubble scale, as shown in figure 1, the upstroke type residual oil hydrogenation reactor 1 comprises an outer cylinder 11, a bubble distribution partition plate 12 is arranged in the outer cylinder 11, the periphery of the bubble distribution partition plate 12 is connected with the inner wall of the outer cylinder 11, a hydrogenation catalyst is filled above the bubble distribution partition plate 12, and a first mixing chamber 13 is arranged below the bubble distribution partition plate 12; a bubbler 14 and a fractal bubble generator 15 are arranged at the bottom end of the outer cylinder 11 in the first mixing cavity 13 and are respectively used for generating large bubbles and micro bubbles distributed in fractal bubbles; a first gas-phase inlet 16, a second gas-phase inlet 17 and a liquid-phase inlet 18 are arranged at the bottom end of the outer cylinder 11, the first gas-phase inlet 16 and the liquid-phase inlet 18 are respectively communicated with a gas-liquid-phase inlet of the fractal bubble generator 15, and the second gas-phase inlet 17 is communicated with the bubbler 14; the top end of the outer cylinder 11 is provided with a discharge hole 19. Raw material residual oil and fresh hydrogen enter the fractal bubble generator 15 to generate raw oil containing micro-fine bubbles, the fresh hydrogen enters the bubbler 14 to generate large bubbles, the large bubbles and the small bubbles are uniformly mixed in the first mixing chamber 13, the mixture passes through the bubble distribution partition plate 12 and then enters a catalyst bed layer to carry out hydrogenation reaction, and a hydrogenation product is discharged from the discharge hole 19.
The fractal bubble distribution is the distribution conforming to one scale fractal, namely the number frequency of bubbles is increased in a power law mode along with the reduction of the diameters of the bubbles, and the power law index is the fractal dimension. The air bubbles distributed in the way are fractal air bubbles, and a great effective mass transfer coefficient can be provided. Specifically, the fractal dimension d is calculated by the following formula:
in the formula: ε is the length of a side of a selected cube, and N is the number of bubbles covered by the cube.
Further, the bubbler 14 is a traditional annular bubbler, and is provided with drum holes with upward openings, the drum holes are distributed along the annular bubbler at equal intervals, and the hole diameter is 2-7 mm.
Further, the fractal bubble generator 15 generates fractal bubbles in a mode of shearing a gas phase through liquid phase rotational flow, the fractal bubble generator 15 is positioned at a central ring of the bubbler 14 and above the bubbler 14, and the distance from the upper end of the fractal bubble generator 15 to the bubble distribution partition plate 12 is 1-4 m.
Further, as shown in fig. 2, a liquid phase tangential inlet 151 is arranged on the side wall of the fractal bubble generator 15, a gas phase axial inlet 152 is arranged at the bottom end of the fractal bubble generator, a second mixing cavity 153 communicating the liquid phase tangential inlet 151 and the gas phase axial inlet 152 is arranged in the fractal bubble generator 15, an air inlet throat 154 is arranged between the gas phase axial inlet 152 and the second mixing cavity 153, a throat outlet 155 is arranged at the upper end of the second mixing cavity 153, and the throat outlet 155 is connected with a spiral shearing blade 156. The raw material residual oil enters the second mixing cavity 153 from the liquid phase tangential inlet 151 to form rotational flow, hydrogen is introduced from the gas phase axial inlet 152, compressed through the gas inlet throat 154 and enters the second mixing cavity 153, a large amount of fractal bubbles are generated under the action of liquid phase rotational flow shearing, the residual oil containing a large amount of fractal bubbles is compressed and discharged from the throat outlet 155, and further sheared into fine bubbles through the rotational flow of the spiral shearing blade 156 to enter the first mixing cavity 13.
Further, the aspect ratio of the second mixing chamber 153, i.e. the ratio of the height to the diameter of the mixing chamber, is (2-4): 1, preferably 2.8: 1; the ratio of the diameter of the inlet throat 154 to the diameter of the second mixing chamber 153 is between 0.05 and 0.3, preferably 0.1; as shown in FIG. 3, the helical shear blade 156 has a helix angle α of 20 to 50, preferably 35.
Further, as shown in fig. 4A and 4B, the bubble distribution partition plate 12 is provided with a plurality of small holes 121, so that the large and small bubbles mixed in the first mixing chamber 13 are uniformly distributed on the catalyst bed layer through the small holes 121, the service efficiency of the catalyst is improved, the aperture of the small holes 121 is 2-4mm, and the distribution form of the small holes 121 is preferably distributed along the center of the partition plate to the periphery at equal intervals. When the height of the catalyst bed is low, specifically, when the height of the catalyst bed is less than 3m, the distribution pattern of the small holes 121 may be selected from a star distribution as shown in fig. 4B, that is, a uniform distribution with equal angles along the center of the partition.
Further, the raw material residual oil is at least one of atmospheric residual oil, vacuum residual oil, deasphalting residual oil and coal tar which are obtained by primary processing or secondary processing, and the density (20 ℃) of the raw material residual oil is 0.89-1.15g/cm 3 Viscosity (100 ℃) is 500- 2 S, having a metal content of less than 150. mu.g/g, preferably less than 100. mu.g/g.
Further, the reaction conditions of the up-flow residual oil hydrogenation reactor 1 are as follows: the reaction pressure is 10-25MPa, the reaction temperature is 300-400 ℃, and the liquid hourly space velocity is 0.2-1.5h -1 And the volume ratio of hydrogen to oil at the inlet of the reactor is 200:1-300:1 (under the standard condition).
The ascending residual oil hydrogenation reactor 1 adopts fractal bubbles and a traditional bubbling mode to carry out combined hydrogenation, and simultaneously generates large bubbles and a large amount of fine bubbles, wherein the fine bubbles are fractal hydrogen bubbles with fractal characteristics in particle size quantity, and the fractal dimension d of the fractal bubbles is not less than 1.5. The liquid phase residual oil containing the mixture of large and small bubbles enters a catalyst bed layer through a bubble distribution clapboard 12 to carry out hydrogenation reaction.
With reference to fig. 5 and 6, the distribution of the bubbles in the catalyst particles 8 is generated by combining the traditional bubbling and the traditional bubbling with the fractal bubbles, compared with the traditional bubbling, the combination of the traditional bubbling and the fractal bubbles is hydrogenated to make the large bubbles and the small bubbles completely cover the surface of the catalyst particles 8, the diameter of the large bubbles 6 is 2-5 times of the catalyst particle gaps, the diameter of the micro bubbles 7 is 0.1-0.3 times of the catalyst particle gaps, a large amount of micro bubbles provide a huge gas-liquid-solid three-phase contact area, and the contact area range reaches 10000- 2 /m 3 So that most of the surface of the catalyst is covered, and the coverage rate of bubbles reaches 70-99%; the large bubbles provide lift force for the small bubbles, and a large amount of carried micro bubbles can quickly replenish hydrogen consumed on the surface of the catalyst, so that the updating of the gas-liquid-solid surface is accelerated, the turbulence of the large bubbles in the rising process improves the fluidity of the whole flow field, and further the mass transfer is enhanced and the liquid phase lifting is promoted.
The above detailed description of the embodiments of the present invention is only for exemplary purposes, and the present invention is not limited to the above described embodiments. Accordingly, variations and modifications in equivalents may be made without departing from the spirit and scope of the invention, which is intended to be covered by the following claims.
Claims (9)
1. An upstroke type residual oil hydrogenation reactor with fractal bubble size is characterized by comprising an outer cylinder, wherein a bubble distribution partition plate is arranged in the outer cylinder, the periphery of the bubble distribution partition plate is connected with the inner wall of the outer cylinder, a hydrogenation catalyst is filled above the bubble distribution partition plate, and a first mixing chamber is arranged below the bubble distribution partition plate; a bubbler and a fractal bubble generator are arranged at the bottom end of the outer barrel in the first mixing cavity; the bottom end of the outer barrel is provided with a first gas phase inlet, a second gas phase inlet and a liquid phase inlet, the first gas phase inlet and the liquid phase inlet are respectively communicated with a gas-liquid phase inlet of the fractal bubble generator, and the second gas phase inlet is communicated with the bubbler; the top end of the outer barrel is provided with a discharge hole.
2. The upflow residuum hydrogenation reactor as in claim 1, wherein the bubbler is an annular bubbler, and the fractal bubble generator is located at a central ring of the bubbler and above the bubbler for shearing a gas phase by a liquid phase cyclone to generate fractal bubbles.
3. The upflow residuum hydrogenation reactor as in claim 2, wherein the upper end of the fractal bubble generator is 1-4m from the bubble distribution baffle.
4. The upflow residuum hydrogenation reactor according to claim 2, characterized in that the bubbler is provided with upward-opening bubbling holes which are equidistantly distributed along the annular bubbler, and the hole diameter is 2-7 mm.
5. The upflow residual oil hydrogenation reactor according to claim 1, characterized in that the side wall of the fractal bubble generator is provided with a liquid phase tangential inlet, the bottom end is provided with a gas phase axial inlet, a second mixing chamber communicating the liquid phase tangential inlet and the gas phase axial inlet is arranged in the fractal bubble generator, an air inlet throat is arranged between the gas phase axial inlet and the second mixing chamber, the upper end of the second mixing chamber is provided with a throat outlet, and the throat outlet is connected with a spiral shearing blade.
6. The upflow residuum hydrogenation reactor as in claim 5, characterized in that the second mixing chamber has an aspect ratio of (2-4): 1; the ratio of the diameter of the air inlet throat to the diameter of the second mixing chamber is 0.05-0.3.
7. The upflow residuum hydrogenation reactor as in claim 5, wherein the helix angle α of the helical shear blades is from 20 ° to 50 °.
8. The upflow residuum hydrogenation reactor as in claim 1, wherein the bubble distribution baffle is provided with a plurality of small holes, and the diameter of the small holes is 2-4 mm.
9. The upflow residuum hydrogenation reactor as in claim 8, wherein the small holes are distributed in an equidistant circumferential distribution from the center of the partition plate to the outer edge.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115445460A (en) * | 2022-08-05 | 2022-12-09 | 中国石油化工股份有限公司 | Tubular gas-liquid mixing and uniform distribution device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115445460A (en) * | 2022-08-05 | 2022-12-09 | 中国石油化工股份有限公司 | Tubular gas-liquid mixing and uniform distribution device |
| CN115445460B (en) * | 2022-08-05 | 2024-01-16 | 中国石油化工股份有限公司 | Tubular gas-liquid mixing and uniformly distributing device |
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