CN210584871U - Multi-scale bubble generation device suitable for strengthening mass transfer of slurry bed - Google Patents
Multi-scale bubble generation device suitable for strengthening mass transfer of slurry bed Download PDFInfo
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- CN210584871U CN210584871U CN201921021667.4U CN201921021667U CN210584871U CN 210584871 U CN210584871 U CN 210584871U CN 201921021667 U CN201921021667 U CN 201921021667U CN 210584871 U CN210584871 U CN 210584871U
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Abstract
The utility model relates to a multi-scale bubble generating device suitable for strengthening mass transfer of a slurry bed, which is provided with a primary distributor, a micro-bubble nozzle, a nozzle distribution disc and a directional bubbling device from bottom to top in sequence; the primary distributor is in communication with a premix gas phase; a liquid phase feeding inlet at the bottom of the slurry bed is arranged at the bottom of the bubble generating device; the directional bubbling device is communicated with the gas-phase feeding inlet; the nozzle distribution disc is uniformly perforated; the liquid phase inlet of the nozzle of the micro-bubble nozzle is arranged at the bottom of the longitudinal section of the nozzle, the gas phase inlet of the nozzle is arranged at the horizontal position of the bottom, and the outlet of the nozzle is arranged at the top; the surface of the directional bubbling device is provided with holes, and the inclination angle theta of the holes is larger than 0 degree and smaller than 180 degrees. The hydrogen of the utility model is dispersed in the residual oil in the form of coexistence of micro bubbles and large bubbles, thereby improving the gas content in the residual oil hydrogenation of the slurry bed and promoting the hydrogenation reaction.
Description
Technical Field
The utility model relates to a strengthen device of thick liquid attitude bed mass transfer more exactly relates to a multiscale bubble produces device suitable for strengthen thick liquid attitude bed mass transfer, belongs to the chemical industry and equips the field.
Background
Petroleum is used as the most widely applied energy in the world, the trend of crude oil heaviness, high acidification and high vulcanization is aggravated at present, along with the increasing strictness of environmental protection regulations and the requirement of petroleum lightening, the conversion efficiency and the processing level of residual oil need to be improved as soon as possible in the world oil refining industry, and the residual oil processing technology can be divided into residual oil hydrogenation and residual oil decarburization. In recent years, the hydrogenation process has been rapidly developed with its treatment effect being remarkable.
The residual oil hydrogenation technology mainly comprises fixed bed hydrogenation treatment, boiling bed hydrocracking, suspension bed hydrocracking, moving bed hydrocracking and slurry bed hydrogenation processes, the former four processes have the defects of low raw material conversion depth, poor adaptability and the like, the slurry bed hydrogenation process has the advantages of high raw material adaptability, high conversion rate and the like, and in recent years, the slurry bed residual oil hydrogenation technology has wide attention at home and abroad, and has good industrial popularization prospect.
The slurry bed is used as an important gas-liquid-solid three-phase reactor, common basic types comprise a bubbling bed reactor, an inner loop flow airlift reactor, an outer loop flow airlift reactor and a spherical reactor, the slurry bed has the advantages of simple structure, uniform dispersion, simplicity and convenience in operation and the like, but the slurry bed has the problems of serious coking, low conversion rate and the like, and the fundamental reason is the defect of hydrogen mass transfer.
The gas distributor inner member is added into the slurry bed reactor, so that the gas feeding can be uniformly distributed in the bed layer, the gas content of the slurry bed can be improved, the mass transfer rate of the slurry bed can be further enhanced, and the one-way conversion rate of liquid can be improved. At present, gas distributors of a slurry bed at home and abroad mainly have two forms, wherein the gas phase enters a slurry bed layer through a nozzle; the other is that the gas phase enters the bed layer of the slurry bed through a distribution disc, but both forms have certain disadvantages, such as the patent with the publication number of CN109317058A, which is named as a novel nozzle for gas distribution of the slurry bed reactor. Although the device has simple and reasonable structure and uniform distribution of gas in the bed layer, the bubbling size is not uniform and basically tends to smaller-size bubbles, and the gas can be reacted at the middle lower part of the bed layer, so that the reaction at the upper part of the bed layer is weak and the mass transfer effect is poor. Also as in patent CN104209069A, entitled slurry bed reactor gas distribution structure. But according to the surface updating gas-liquid mass transfer theory, the single reduction of the bubble size can not meet the requirements of slurry bed hydrogenation mass transfer.
SUMMERY OF THE UTILITY MODEL
In view of the above problems and the related theories, the utility model provides a technique for completing the hydrogenation of the residual oil in a slurry bed to generate multi-scale bubbles by using the combination of a micro-bubble nozzle and a bubbling ring. Based on microbubble generation and the tympanic bulla production principle, the utility model discloses can accomplish. The device has the advantages of large quantity of bubbles, small average size of the bubbles, small rising speed of the bubbles, long retention time, increased gas-liquid contact area, strengthened mass transfer among all phases of a slurry bed, promoted hydrogenation reaction, improved conversion rate of residual oil hydrogenation and the like.
The utility model discloses a concrete technical scheme as follows:
a multi-scale bubble generating device suitable for strengthening mass transfer of a slurry bed is provided with a primary distributor 5, a micro-bubble nozzle 2, a nozzle distribution plate 3 and a directional bubbling device 4 from bottom to top in sequence;
the primary distributor 5 is in communication with the premix gas phase; a liquid phase feeding inlet 1 at the bottom of the slurry bed is arranged at the bottom of the bubble generating device; the directional bubbling device 4 is communicated with a gas-phase feeding inlet;
the nozzle distribution plate 3 is uniformly perforated;
the nozzle liquid phase inlet 21 of the micro-bubble nozzle 2 is arranged at the bottom of the longitudinal section of the nozzle, the nozzle gas phase inlet 22 is arranged at the horizontal position of the bottom, and the nozzle outlet 23 is arranged at the top;
the surface of the directional bubbling device 4 is provided with holes 41, and the inclination angle theta of the holes is larger than 0 degree and smaller than 180 degrees.
The poor residual oil enters the bottom of the reactor from a liquid phase inlet at the bottom of the slurry bed, and the premixed hydrogen forms a gas-liquid mixture at the bottom of the reactor through a primary distributor; poor-quality residual oil and premixed hydrogen enter a flow guide inlet of the nozzle; residual oil and hydrogen entering the nozzle are sprayed out from the nozzle outlet to generate micro bubbles, and the generated micro bubbles of premixed hydrogen rise along with the flowing of a liquid phase; additionally supplementing hydrogen into the directional bubbling device; the bigger bubbles generated by the bubbling device are uniformly mixed with the micro-bubbles generated by the nozzle and rise.
Further, the number of the openings of the nozzle distribution plate 3 is between the liquid phase flow rate/20 square per hour and the liquid phase flow rate/0.2 square per hour.
Further, the minimum flow passage size of the micro-bubble nozzle 2 and the directional bubbling device 4 is not less than 3mm, and the processing material should have corrosion resistance.
The utility model is suitable for a multiscale bubble production method of reinforcing slurry bed mass transfer, including following step:
(1) firstly, residual oil raw materials enter the bottom of a reactor from the bottom of a slurry bed, premixed hydrogen passes through a primary distributor to form a gas-liquid mixture at the bottom of the reactor, and hydrogen-oil premixing is completed;
(2) forming a hydrogen gas cushion protective atmosphere below the partition plate, and enabling liquid-phase residual oil and premixed hydrogen to enter a flow guide inlet of the nozzle; residual oil and hydrogen entering the nozzle are sprayed out from the nozzle outlet to generate micro bubbles, and the generated micro bubbles of premixed hydrogen flow upwards along with the liquid phase flow;
(3) supplementing hydrogen into the directional bubbling device; the bigger bubbles generated by the bubbling device are uniformly mixed with the micro-bubbles generated by the nozzle and rise.
Further, in the step (1), the hydrogen pressure drop of the primary distributor at the bottom of the reactor is not less than 0.2 KPa.
Further, in the step (2), the liquid phase speed of a diversion inlet of the nozzle is 3-15m/s, the gas-liquid volume flow ratio at the diversion inlet is 50 at most, and micro-bubbles of 10-2000 microns can be generated.
Further, in the step (3), the pressure drop of the hydrogen of the directional bubbling device is not lower than 30% of the pressure caused by the height of the liquid phase of the reactor, and the diameter of generated bubbles is 2-100 mm.
Further, the primary distributor in the step (1) is connected with the bottom of the slurry bed by adopting a welding connection method.
Further, the nozzles in the step (1) are vertically arranged on a nozzle distribution disc, and the nozzle distribution disc is connected with the inner wall of the slurry bed by adopting a welding method.
Further, the nozzle in the step (1) has the same structure size, the low-position installation of 1-15 vortex members is reserved, and the shutdown and complete material returning of the reactor are realized.
Further, the vertical distance between the top of the nozzle in the step (1) and the directional bubbling device in the step (3) is 100 mm-0.1 time of the internal diameter of the slurry bed reactor.
The beneficial effects of the utility model reside in that:
(1) the residual oil mixed with the catalyst and the hydrogen are fully mixed in the microbubble nozzle, and the hydrogen exists in the residual oil in the form of microbubbles, so that the gas content in the residual oil hydrogenation of a slurry bed is improved, the retention time is long, and the gas-liquid contact area is increased.
(2) The existence of larger bubbles improves the liquid phase mass transfer coefficient of the slurry bed hydrogenation reaction, strengthens the mass transfer among all phases of the slurry bed and improves the conversion rate of residual oil hydrogenation.
(3) The mass transfer coefficient is improved on the whole, the utilization rate of hydrogen in the slurry bed residual oil hydrogenation process is improved, the hydrogen-oil ratio is reduced, and the operation cost is saved.
Drawings
FIG. 1 is a schematic view of the structure of an apparatus according to example 1;
fig. 2 is a schematic sectional view of the structure of the microbubble nozzle 2;
fig. 3 is a schematic top view of the nozzle distribution plate 3;
fig. 4 is a schematic structural view of the directional bubbling device 4;
description of the symbols:
1-a liquid phase inlet at the bottom of the slurry bed; 2-a micro-bubble nozzle; 3-nozzle distribution plate; 4-a directional bubbling device; 5-a primary distributor; 21-nozzle liquid phase inlet; 22-nozzle gas phase inlet; 23-nozzle outlet; 41-surface opening of the directional bubbling device.
Detailed Description
The present invention will be described in detail with reference to the following examples. It is necessary to point out here that the following examples are only used for further illustration of the present invention, and should not be interpreted as limiting the scope of the present invention, and that the skilled person in this field may make some insubstantial modifications and adjustments according to the contents of the present invention, and still fall within the scope of the present invention.
Example 1
At present, the gas distributor of the slurry bed at home and abroad mainly has two forms, one is that gas phase enters the bed layer of the slurry bed through a nozzle; the other is that the gas phase enters the slurry bed layer through a distribution plate. However, both methods have many disadvantages, for example, the gas phase enters the slurry bed layer through the nozzle, the bubble size is not uniform and basically tends to small bubbles, the gas can be reacted at the middle lower part of the bed layer, the reaction at the upper part of the bed layer is weak, and the mass transfer effect is poor; if the gas phase enters the slurry bed layer through the distribution disc, the bubble size is larger, the rising speed of the bubble is high, the retention time is short, the gas-liquid contact area is small, the mass transfer effect is poor, and the product conversion rate is lower. The method of combining the micro-bubble generation and the bubbling ring is adopted, hydrogen exists in residual oil in a micro-bubble mode, the gas content rate in residual oil hydrogenation of a slurry bed is improved, the number of bubbles is large, the average size of the bubbles is small, the rising speed of the micro-bubbles is small, the retention time is long, the gas-liquid contact area is increased, the mass transfer among all phases of the slurry bed is enhanced, the conversion rate of residual oil hydrogenation is improved, the utilization rate of the hydrogen during residual oil hydrogenation of the slurry bed is improved, and the hydrogen-oil ratio is reduced. Based on the above discovery, the utility model discloses can accomplish.
As shown in fig. 1, which is a schematic structural view of embodiment 1 of the present invention, the slurry bed multi-scale bubble generating device mainly includes a micro-bubble nozzle 2; a nozzle distribution plate 3; the bubbling device 4 is oriented. The multi-scale bubble generation device is adopted by a certain petrochemical plant to carry out residual oil hydrogenation in a slurry bed, and the properties and the operating conditions of the residual oil are shown in the following table:
TABLE 1 residual oil Properties
| Density (20 ℃), kg.m-3 | 1025.6 |
| Residual carbon number, wt% | 18.9 |
| S,wt％ | 2.8 |
| N,wt％ | 0.38 |
| Metallic element, ug/g | |
| Fe | 2.9 |
| Ni | 38.7 |
| V | 286.4 |
| Gum, wt% | 25.7 |
| Asphaltenes, wt.% | 13.8 |
TABLE 2 operating conditions
| Reaction temperature of | 430 |
| Reaction pressure, MPa | 16 |
| Volume ratio of hydrogen to oil, v/v | 950 |
Firstly, the inferior residual oil enters the reactor from a liquid phase inlet at the bottom of a slurry bed, the inlet flow rate of the residual oil is controlled to be 2-5m/s, the inferior residual oil in the reactor enters a liquid phase inlet of a nozzle, and hydrogen enters the nozzle from a gas phase inlet of the nozzle to complete hydrogen-oil premixing. Residual oil and hydrogen gas entering the nozzle are sprayed out from the nozzle outlet to generate micro-bubbles of 10-45 microns, and the generated micro-bubbles rise along with the flowing of a liquid phase. Hydrogen enters the bubbling ring from the inlet of the bubbling ring and is discharged from the upper gas-phase outlet of the bubbling ring, and bubbles of 3-10cm are generated. As the residuum flows, the bubbles and microbubbles mix uniformly and rise.
When the method and the device are used for carrying out residual oil hydrogenation on a slurry bed, the volume ratio of hydrogen to oil is reduced from 980 to 950, and the residual oil conversion rate is improved from 68% to 74%.
The utility model has the main advantages that:
the catalyst mixed residual oil and hydrogen of the utility model are fully mixed in the micro-bubble nozzle, and the hydrogen exists in the residual oil in the form of micro-bubbles, thereby improving the gas content in the residual oil hydrogenation of the slurry bed and promoting the hydrogenation reaction; when the slurry bed is subjected to hydrogenation reaction, the number of bubbles is large, the average size of the bubbles is small, the rising speed of micro bubbles is small, the retention time is long, the gas-liquid contact area is increased, the mass transfer among all phases of the slurry bed is enhanced, and the conversion rate of residual oil hydrogenation is improved; the utilization rate of hydrogen in the slurry bed residual oil hydrogenation process is improved, the hydrogen-oil ratio is reduced, and the operation cost is saved.
Claims (2)
1. A multi-scale bubble generating device suitable for strengthening mass transfer of a slurry bed is characterized in that a primary distributor, a micro-bubble nozzle, a nozzle distribution disc and a directional bubbling device are sequentially arranged on the device from bottom to top;
the primary distributor is in communication with a premix gas phase; a liquid phase feeding inlet at the bottom of the slurry bed is arranged at the bottom of the bubble generating device; the directional bubbling device is communicated with the gas-phase feeding inlet;
the nozzle distribution disc is uniformly perforated;
the liquid phase inlet of the nozzle of the micro-bubble nozzle is arranged at the bottom of the longitudinal section of the nozzle, the gas phase inlet of the nozzle is arranged at the horizontal position of the bottom, and the outlet of the nozzle is arranged at the top;
the surface of the directional bubbling device is provided with holes, and the inclination angle theta of the holes is larger than 0 degree and smaller than 180 degrees.
2. The multi-scale bubble generation device suitable for enhancing the mass transfer of the slurry bed according to claim 1, wherein the vertical distance between the top of the nozzle and the directional bubbling device is 100 mm-0.1 times the inner diameter of the slurry bed reactor.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110270280A (en) * | 2019-07-03 | 2019-09-24 | 上海米素环保科技有限公司 | A kind of multiple dimensioned bubble production method and device suitable for strengthening slurry bed system mass transfer |
| CN114196433A (en) * | 2021-12-29 | 2022-03-18 | 华东理工大学 | Hydrocracking reaction process and fluidized bed reactor for hydrocracking |
| CN115093880A (en) * | 2022-07-31 | 2022-09-23 | 中国石油化工股份有限公司 | Mixed bubble flow fluidized bed residual oil hydrogenation process and device |
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2019
- 2019-07-03 CN CN201921021667.4U patent/CN210584871U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110270280A (en) * | 2019-07-03 | 2019-09-24 | 上海米素环保科技有限公司 | A kind of multiple dimensioned bubble production method and device suitable for strengthening slurry bed system mass transfer |
| CN110270280B (en) * | 2019-07-03 | 2024-07-09 | 上海米素环保科技有限公司 | Multi-scale bubble generation method and device suitable for strengthening mass transfer of slurry bed |
| CN114196433A (en) * | 2021-12-29 | 2022-03-18 | 华东理工大学 | Hydrocracking reaction process and fluidized bed reactor for hydrocracking |
| CN115093880A (en) * | 2022-07-31 | 2022-09-23 | 中国石油化工股份有限公司 | Mixed bubble flow fluidized bed residual oil hydrogenation process and device |
| CN115093880B (en) * | 2022-07-31 | 2024-03-19 | 中国石油化工股份有限公司 | Mixed bubble flow ebullated bed residual oil hydrogenation process and device |
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Effective date of registration: 20220809 Address after: 201514 room 3533, building 1, No. 2758, Songjin Road, Zhangyan Town, Jinshan District, Shanghai Patentee after: SHANGHAI MISU ENVIRONMENTAL PROTECTION TECHNOLOGY Co.,Ltd. Patentee after: Ji'an Yonglan (Beijing) Engineering Technology Development Co.,Ltd. Patentee after: SINOPEC ENGINEERING Inc. Address before: 201514 room a3533, building 1, 2758 Songjin Road, Zhangyan Town, Jinshan District, Shanghai Patentee before: SHANGHAI MISU ENVIRONMENTAL PROTECTION TECHNOLOGY Co.,Ltd. Patentee before: Ji'an Yonglan (Beijing) Engineering Technology Development Co.,Ltd. |