CN214346338U - Combined upflow reactor with multiple partitions - Google Patents
Combined upflow reactor with multiple partitions Download PDFInfo
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- CN214346338U CN214346338U CN202022583238.5U CN202022583238U CN214346338U CN 214346338 U CN214346338 U CN 214346338U CN 202022583238 U CN202022583238 U CN 202022583238U CN 214346338 U CN214346338 U CN 214346338U
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Abstract
The utility model relates to a petrochemical technical field, concretely relates to combination formula upflow reactor who sets up a plurality of subregion, include ebullated bed reactor and set up the suspension bed reactor in ebullated bed reactor, ebullated bed reactor includes ebullated bed pressure-bearing casing, set up in the distribution plate of ebullated bed pressure-bearing casing lower part and set up in the ebullated bed gas-liquid separator on upper portion in the ebullated bed pressure-bearing casing, suspension bed reactor includes the suspension bed reactor casing, set up in the cone feeding section of suspension bed reactor casing bottom, set up in the liquid phase circulation backward flow mouth at suspension bed reactor casing middle part, set up in the liquid phase back flow of suspension bed reactor casing one side and set up in the suspension bed gas-liquid separator at suspension bed reactor casing top. The utility model discloses the mass transfer and the heat transfer process of gas-liquid material in the reactor have been strengthened for reaction temperature is more even, and the reaction heat diffuses more easily, and the gaseous reactor that leaves that produces of reaction is faster.
Description
Technical Field
The utility model relates to a petrochemical technical field, concretely relates to combination formula upflow reactor who sets up a plurality of subregion.
Background
The gas content and the liquid phase back mixing degree of the upflow reactor have a very close relation with the gas phase apparent flow rate. The higher the apparent flow rate of the gas phase, the higher the gas content and the higher the degree of back-mixing of the liquid phase.
The degree of liquid phase back mixing is directly related to the radial gas distribution of the reactor. Generally, the gas of the upflow reactor enters from the central position of the bottom, which causes the gas content at the center of the reactor to be high, the gas content near the wall to be low, and the difference of the gas content causes the liquid phase to form back mixing.
The liquid phase back mixing enhances the mass transfer and heat transfer process of gas-liquid materials in the reactor, so that the reaction temperature is more uniform, the reaction heat is easier to diffuse, and the gas generated by the reaction leaves the reactor more quickly.
The lower section of the upflow reactor has violent reaction because of high concentration of the reactive fresh materials and needs large liquid phase back mixing to take away the reaction heat; in the upper half of the upflow reactor, the reaction becomes more moderate due to the lower concentration of the reactable material, and higher catalyst concentration and lower liquid phase back-mixing are required to improve the reaction depth.
Therefore, according to the different reaction characteristic requirements of the lower section and the upper section of the upflow reactor, a new upflow reactor type is needed to meet the above reaction characteristic requirements.
Disclosure of Invention
In order to overcome the defects and shortcomings in the prior art, the utility model aims to provide a combined upflow reactor with a plurality of subareas.
The purpose of the utility model is realized through the following technical scheme: a combined up-flow reactor with a plurality of subareas comprises a fluidized bed reactor and a suspended bed reactor arranged in the fluidized bed reactor, wherein the fluidized bed reactor comprises a fluidized bed pressure-bearing shell, a distribution plate arranged at the lower part in the fluidized bed pressure-bearing shell and a fluidized bed gas-liquid separator arranged at the upper part in the fluidized bed pressure-bearing shell, the suspended bed reactor comprises a suspended bed reactor shell, a cone feeding section arranged at the bottom of the suspended bed reactor shell, a liquid phase circulating reflux port arranged at the middle part of the suspended bed reactor shell, a liquid phase reflux pipe arranged at one side of the suspended bed reactor shell and a suspended bed gas-liquid separator arranged at the top of the suspended bed reactor shell, the distribution plate is arranged between the outer side wall of the suspended bed reactor shell and the inner side wall of the fluidized bed pressure-bearing shell, the distribution plate is provided with a plurality of through holes penetrating through the upper and lower surfaces of the distribution plate, and the bottom of the fluidized bed pressure-bearing shell is provided with a raw material inlet, the top of the fluidized bed pressure-bearing shell is provided with a gas outlet, the side wall of the fluidized bed pressure-bearing shell is provided with a plurality of cold hydrogen inlets, the fluidized bed gas-liquid separator is provided with a liquid outlet, and the cone feeding section is connected with the raw material inlet.
Furthermore, a suspension bed fast fluidized reaction zone is arranged at the lower part in the shell of the suspension bed reactor, a suspension bed gas-liquid separation zone is arranged above the shell of the suspension bed reactor, a boiling bed liquid phase retention zone, a boiling bed catalyst dense phase zone and a boiling bed catalyst dilute phase zone are sequentially arranged between the outer side wall of the shell of the suspension bed reactor and the inner side wall of the boiling bed pressure-bearing shell from bottom to top, the boiling bed liquid phase retention zone is positioned below the distribution plate, and the boiling bed catalyst dense phase zone and the boiling bed catalyst dilute phase zone are positioned above the distribution plate.
Furthermore, the top of the distribution plate is filled with a solid catalyst, and the particle size of the solid catalyst is larger than the aperture of the through hole.
Further, the particle size of the solid catalyst ranges from 1 mm to 10mm, and the solid catalyst is cylindrical, spherical or cloverleaf-shaped.
Further, the solid catalyst is a hydrofining catalyst or a hydrocracking catalyst.
Furthermore, the hydrofining catalyst is a solid catalyst of carrier amorphous alumina or aluminosilicate loaded with active metal nickel, molybdenum, cobalt or tungsten.
Further, the hydrocracking catalyst is a solid catalyst which has acidic centers and is prepared by loading active metal nickel, molybdenum, cobalt or tungsten on a carrier amorphous aluminosilicate or a molecular sieve.
The beneficial effects of the utility model reside in that: the utility model discloses a combination formula upflow reactor adopts ebullated bed reactor and sets up the suspension bed reactor in ebullated bed reactor to cut apart into center fast fluidization district, catalyst dense phase reaction zone, catalyst dilute phase reaction zone and gas-liquid separation district with combination formula upflow reactor through the distributing plate, strengthened the mass transfer and the heat transfer process of gas-liquid material in the reactor, make reaction temperature more even, the reaction heat diffuses more easily, the gaseous reactor that leaves that produces of reaction is faster.
The combined upflow reactor of the utility model has the following advantages:
1) the raw materials and hydrogen are high back-mixed by utilizing the characteristic of a fast fluidized zone of a suspension bed, and the heat transfer and mass transfer are fast in the reaction process; the utility model is particularly suitable for the reaction process of violent exothermic reaction, easy condensation and easy temperature runaway of materials. For example, biological raw oil such as high oxygen-containing oil and fat, wood tar and the like, and secondary processed raw oil such as catalytic gasoline and diesel oil, coking gasoline and diesel oil, ethylene cracking tar, fast pyrolysis coal tar and the like with high unsaturated hydrocarbon content.
2) A liquid phase reflux port is arranged on the shell of the suspension bed reactor, and the liquid self-circulation process from the liquid circulation in the fluidized bed to the suspension bed can be realized by utilizing the density difference of the suspension bed and the fluidized bed caused by different gas content; the utility model discloses can realize circulating fluidized bed liquid phase product to suspension bed part, this part circulating oil can regard as the hydrogen donor solvent of suspension bed reaction part.
3) The reaction gas phase product of the suspension bed rapidly leaves the reactor. The utility model discloses be favorable to the quick derivation of gaseous impurity in the suspension bed reaction product. The utility model is particularly suitable for the processing of high oxygen-containing compounds, and the suspension bed reaction generates H2O、CO、CO2And the impurity gas can be quickly led out of the reaction system, so that the adverse effect of the part of the impurity gas on the catalyst and the reaction is reduced.
4) The liquid phase is connected to a liquid phase retention area of the boiling bed through a liquid phase return pipe and enters the boiling bed for further reaction;
5) the middle lower part of the fluidized bed is provided with a distribution plate to realize the uniform distribution of gas-liquid phases;
6) because the gas-liquid ratio in the boiling bed is obviously reduced, the catalyst realizes the concentration difference of catalyst distribution in the vertical direction, the bottom is a catalyst dense-phase zone, and the upper part is a catalyst dilute-phase zone.
Drawings
Fig. 1 is a schematic structural diagram of the combined upflow reactor of the present invention.
Fig. 2 is a schematic structural diagram of a cross section of the combined upflow reactor of the present invention.
The reference signs are: the fluidized bed reactor comprises a fluidized bed reactor 1, a fluidized bed pressure-bearing shell 11, a distribution plate 12, a fluidized bed gas-liquid separator 13, a suspended bed reactor 2, a suspended bed reactor shell 21, a cone feeding section 22, a liquid phase circulating reflux port 23, a liquid phase reflux pipe 24 and a suspended bed gas-liquid separator 25;
a raw material inlet 101, a gas outlet 102, a cold hydrogen inlet 103, a liquid outlet 104, a suspension bed fast fluidization reaction zone 105, a suspension bed gas-liquid separation zone 106, an ebullated bed liquid phase residence zone 107, an ebullated bed catalyst dense-phase zone 108 and an ebullated bed catalyst dilute-phase zone 109.
Detailed Description
In order to facilitate the understanding of those skilled in the art, the present invention will be further described with reference to the following examples and accompanying fig. 1-2, which are not intended to limit the present invention.
Referring to fig. 1-2, a combined up-flow reactor with a plurality of partitions comprises a fluidized bed reactor 1 and a suspended bed reactor 2 arranged in the fluidized bed reactor 1, wherein the fluidized bed reactor 1 comprises a fluidized bed pressure-bearing shell 11, a distribution plate 12 arranged at the lower part in the fluidized bed pressure-bearing shell 11 and a fluidized bed gas-liquid separator 13 arranged at the upper part in the fluidized bed pressure-bearing shell 11, the suspended bed reactor 2 comprises a suspended bed reactor shell 21, a cone feeding section 22 arranged at the bottom of the suspended bed reactor shell 21, a liquid phase circulating reflux opening 23 arranged at the middle part of the suspended bed reactor shell 21, a liquid phase reflux pipe 24 arranged at one side of the suspended bed reactor shell 21 and a suspended bed gas-liquid separator 25 arranged at the top of the suspended bed reactor shell 21, the distribution plate 12 is arranged between the outer side wall of the suspended bed reactor shell 21 and the inner side wall of the fluidized bed pressure-bearing shell 11, the distribution plate 12 is provided with a plurality of through holes penetrating through the upper surface and the lower surface of the distribution plate, the bottom of the fluidized bed pressure-bearing shell 11 is provided with a raw material inlet 101, the top of the fluidized bed pressure-bearing shell 11 is provided with a gas outlet 102, the side wall of the fluidized bed pressure-bearing shell 11 is provided with a plurality of cold hydrogen inlets 103, the fluidized bed gas-liquid separator 13 is provided with a liquid outlet 104, and the cone feeding section 22 is connected with the raw material inlet 101.
In this embodiment, a suspension bed fast fluidized reaction zone 105 is disposed at the lower portion inside the suspension bed reactor housing 21, a suspension bed gas-liquid separation zone 106 is disposed above the suspension bed reactor housing 21, a fluidized bed liquid phase retention zone 107, a fluidized bed catalyst dense phase zone 108, and a fluidized bed catalyst dilute phase zone 109 are sequentially disposed between the outer side wall of the suspension bed reactor housing 21 and the inner side wall of the fluidized bed pressure-bearing housing 11 from bottom to top, the fluidized bed liquid phase retention zone 107 is located below the distribution plate 12, and the fluidized bed catalyst dense phase zone 108 and the fluidized bed catalyst dilute phase zone 109 are located above the distribution plate 12.
The utility model discloses a combination formula upflow reactor adopts ebullated bed reactor 1 and sets up the suspension bed reactor 2 in ebullated bed reactor 1, and cut apart into central fast fluidization district (the fast fluidization reaction zone 105 of suspension bed) with combination formula upflow reactor through distributing plate 12, catalyst dense phase reaction zone (ebullated bed catalyst dense phase district 108), catalyst dilute phase reaction zone (ebullated bed catalyst dilute phase district 109) and gas-liquid separation district (suspension bed gas-liquid separation district 106), the mass transfer and the heat transfer process of gas-liquid material in the reactor have been strengthened, make reaction temperature more even, the reaction heat diffuses more easily, the gaseous reactor that leaves that produces of reaction sooner.
In this embodiment, the top of the distribution plate 12 is filled with a solid catalyst, and the particle size of the solid catalyst is larger than the aperture of the through hole. The arrangement of the above structure can prevent the solid catalyst from falling.
In this example, the particle size of the solid catalyst ranges from 1 mm to 10mm, and the solid catalyst is cylindrical, spherical or cloverleaf.
The distribution plate 12 may serve the following functions: 1) supporting the upper large particle solid catalyst; 2) realizing redistribution of gas, liquid and solid in the pre-reaction section; 3) prevent the solid catalyst with large particles on the upper part from falling to the pre-reaction section. The distribution plate 12 preferably adopts a distribution plate 12 structure with a plurality of cap distributors.
In this embodiment, the solid catalyst is a hydrofining catalyst or a hydrocracking catalyst. The hydrofining catalyst realizes the further hydrogenation process of the product in the pre-reaction section; the hydrocracking catalyst realizes the hydrocracking process of the products in the pre-reaction section.
In this embodiment, the hydrorefining catalyst is a solid catalyst in which active metals nickel, molybdenum, cobalt, or tungsten are supported on amorphous alumina or aluminosilicate as a carrier.
In this embodiment, the hydrocracking catalyst is a solid catalyst in which active metals nickel, molybdenum, cobalt, or tungsten are supported on a carrier amorphous aluminosilicate or molecular sieve having an acid center.
The above-mentioned embodiment is the utility model discloses the implementation of preferred, in addition, the utility model discloses can also realize by other modes, not deviating from the utility model discloses any obvious replacement is all within the protection scope under the prerequisite of design.
Claims (5)
1. A modular upflow reactor with multiple zones, comprising: the fluidized bed reactor comprises a fluidized bed reactor and a suspended bed reactor arranged in the fluidized bed reactor, wherein the fluidized bed reactor comprises a fluidized bed pressure-bearing shell, a distribution plate arranged at the lower part in the fluidized bed pressure-bearing shell and a fluidized bed gas-liquid separator arranged at the upper part in the fluidized bed pressure-bearing shell, the suspended bed reactor comprises a suspended bed reactor shell, a cone feeding section arranged at the bottom of the suspended bed reactor shell, a liquid phase circulating reflux opening arranged at the middle part of the suspended bed reactor shell, a liquid phase reflux pipe arranged at one side of the suspended bed reactor shell and a suspended bed gas-liquid separator arranged at the top of the suspended bed reactor shell, the distribution plate is arranged between the outer side wall of the suspended bed reactor shell and the inner side wall of the fluidized bed pressure-bearing shell, the distribution plate is provided with a plurality of through holes penetrating through the upper surface and the lower surface of the distribution plate, the bottom of the fluidized bed pressure-bearing shell is provided with a raw material inlet, and the top of the fluidized bed pressure-bearing shell is provided with a gas outlet, the side wall of the pressure-bearing shell of the fluidized bed is provided with a plurality of cold hydrogen inlets, the gas-liquid separator of the fluidized bed is provided with a liquid outlet, and the cone feeding section is connected with the raw material inlet.
2. A modular upflow reactor with multiple zones as in claim 1, in which: the fluidized bed reactor is characterized in that a suspension bed fast fluidized reaction zone is arranged at the lower part in the shell of the suspension bed reactor, a suspension bed gas-liquid separation zone is arranged above the shell of the suspension bed reactor, a boiling bed liquid phase retention zone, a boiling bed catalyst dense-phase zone and a boiling bed catalyst dilute-phase zone are sequentially arranged between the outer side wall of the shell of the suspension bed reactor and the inner side wall of a boiling bed pressure-bearing shell from bottom to top, the boiling bed liquid phase retention zone is positioned below the distribution plate, and the boiling bed catalyst dense-phase zone and the boiling bed catalyst dilute-phase zone are positioned above the distribution plate.
3. A modular upflow reactor with multiple zones as in claim 1, in which: and the top of the distribution plate is filled with a solid catalyst, and the particle size of the solid catalyst is larger than the aperture of the through hole.
4. A modular upflow reactor with multiple zones as in claim 3, in which: the particle size range of the solid catalyst is 1-10mm, and the solid catalyst is cylindrical, spherical or cloverleaf.
5. A modular upflow reactor with multiple zones as in claim 3, in which: the solid catalyst is a hydrofining catalyst or a hydrocracking catalyst.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022583238.5U CN214346338U (en) | 2020-11-10 | 2020-11-10 | Combined upflow reactor with multiple partitions |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022583238.5U CN214346338U (en) | 2020-11-10 | 2020-11-10 | Combined upflow reactor with multiple partitions |
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| Publication Number | Publication Date |
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| CN214346338U true CN214346338U (en) | 2021-10-08 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202022583238.5U Active CN214346338U (en) | 2020-11-10 | 2020-11-10 | Combined upflow reactor with multiple partitions |
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| CN (1) | CN214346338U (en) |
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- 2020-11-10 CN CN202022583238.5U patent/CN214346338U/en active Active
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| TR01 | Transfer of patent right |
Effective date of registration: 20220901 Address after: No. 8, South 1st Row, Xinxing Road, Xinle City, Shijiazhuang City, Hebei Province, 050000 Patentee after: Shijiazhuang Ruitu Biotechnology Co.,Ltd. Address before: 570000 201, building B, National University Science Park, Hainan Normal University, No. 3, Haitao Avenue, Jiangdong new area, Haikou City, Hainan Province Patentee before: Hainan Bailang Biotechnology Co.,Ltd. |
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| TR01 | Transfer of patent right |
Effective date of registration: 20220920 Address after: 201913 No. 495, Yuejin South Road, Xinhai Town, Chongming District, Shanghai (Guangming Rice Industry Economic Park) Patentee after: Shanghai Kered Energy Technology Co.,Ltd. Address before: No. 8, South 1st Row, Xinxing Road, Xinle City, Shijiazhuang City, Hebei Province, 050000 Patentee before: Shijiazhuang Ruitu Biotechnology Co.,Ltd. |
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