CN115738905A - Inlet diffuser for heavy raw oil hydrogenation reaction and hydrogenation reactor - Google Patents
Inlet diffuser for heavy raw oil hydrogenation reaction and hydrogenation reactor Download PDFInfo
- Publication number
- CN115738905A CN115738905A CN202211363705.0A CN202211363705A CN115738905A CN 115738905 A CN115738905 A CN 115738905A CN 202211363705 A CN202211363705 A CN 202211363705A CN 115738905 A CN115738905 A CN 115738905A
- Authority
- CN
- China
- Prior art keywords
- oil
- diameter
- spoiler
- inlet diffuser
- hydrogenation reaction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 55
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 2
- 239000003129 oil well Substances 0.000 claims 1
- 238000009826 distribution Methods 0.000 abstract description 8
- 230000000694 effects Effects 0.000 abstract description 8
- 239000012530 fluid Substances 0.000 abstract description 8
- 238000009792 diffusion process Methods 0.000 abstract description 6
- 239000006185 dispersion Substances 0.000 abstract description 5
- 239000003921 oil Substances 0.000 description 74
- 239000007789 gas Substances 0.000 description 50
- 238000005457 optimization Methods 0.000 description 15
- 230000000052 comparative effect Effects 0.000 description 8
- 239000003054 catalyst Substances 0.000 description 6
- 238000009434 installation Methods 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 238000002474 experimental method Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000000295 fuel oil Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000009827 uniform distribution Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model provides a heavy matter raw oil hydrogenation is with entry diffuser and hydrogenation ware, belongs to the hydrogenation subassembly among the petrochemical industry field, including barrel and the striking plate of setting in barrel oil gas export below, the cylinder is internal to have set gradually upper spoiler, lower spoiler and cowling panel along the oil gas flow direction, and wherein, upper spoiler, lower spoiler are the annular slab of level setting in the barrel, and the cowling panel is the little diameter end open-ended obround shape in bottom, and its surface gathers there is the slit. The inlet diffuser is provided with the two layers of spoilers and the two layers of rectifying plates, so that fluid deflected on one side is subjected to twice correction and then is subjected to diffusion distribution on the impact disc, a good correction effect is achieved on the deflected flow, and the dispersion is better.
Description
Technical Field
The invention relates to a hydrogenation reaction in the field of petrochemical industry, in particular to an inlet diffuser for the hydrogenation reaction of heavy raw oil and a hydrogenation reactor.
Background
The wax oil hydrogenation device provides raw materials for the FCC device by carrying out reactions such as desulfurization, denitrification, demetalization and the like on the vacuum wax oil. With the continuous deterioration of crude oil, the sulfur and nitrogen contents of the vacuum wax oil are obviously increased, the metal content, colloid content and asphaltene content are also obviously increased, and mechanical impurities such as coke powder and the like cannot be completely removed from the raw materials, so that higher technical requirements are put forward in the field of wax oil hydrotreatment.
At present, the upgrading and optimizing directions of the wax oil hydrogenation technology are mainly as follows:
1. the method solves the problems of poor raw material quality, harsh production index and short running period by updating the wax oil hydrogenation catalyst;
2. optimizing a wax oil hydrogenation process, including optimizing a heat exchange process, reducing coking in a heating furnace and a pipeline and the like;
3. a novel wax oil hydrogenation process is provided, such as liquid phase circulation hydrogenation, hydrogenation reaction is carried out through hydrogen carried by a large amount of products in a circulation mode, the integral temperature rise of a reactor is controllable, and coking and blocking of a bed layer are reduced.
Good process and catalyst are matched with good engineering technology to achieve the best effect. The inlet diffuser is the first internal member installed at the reactor inlet and plays an extremely important role in the initial distribution of the feedstock within the reactor. The inlet diffusers mentioned in the prior publications and documents have good initial distribution effect on light raw materials, but the high density and high viscosity of the wax oil cause that the wax oil is more prone to drift and difficult to disperse in the feeding process, and higher requirements on dispersion and uniform distribution are provided.
Disclosure of Invention
In order to solve the problem that the inlet diffuser in the prior art is more prone to bias flow and difficult to disperse for heavy raw oil such as wax oil with high density and high viscosity, the invention provides the inlet diffuser and the hydrogenation reactor for the hydrogenation reaction of the heavy raw oil.
The technical scheme adopted by the invention for solving the technical problems is as follows: the utility model provides a heavy raw oil hydrogenation is with entry diffuser, includes the barrel and sets up the impingement plate in barrel oil gas export below, the interior spoiler, lower spoiler and the cowling panel of having set gradually along the oil gas flow direction of following of barrel, wherein, go up spoiler, lower spoiler and be the annular plate of level setting in the barrel, the cowling panel is the little diameter end open-ended obround shape in bottom, and its surface gathers there is the slit.
As an optimization scheme of the inlet diffuser for the hydrogenation reaction of the heavy raw oil, the diameter of the bottom opening of the rectifying plate is smaller than the diameters of the inner rings of the upper spoiler and the lower spoiler, and the diameter of the inner ring of the upper spoiler is not smaller than the diameter of the inner ring of the lower spoiler.
As another optimization scheme of the inlet diffuser for the hydrogenation reaction of the heavy raw oil, the included angle between the generatrix of the rectifying plate and the inner wall of the cylinder body is 40-60 degrees, and preferably 45 degrees.
As another optimization scheme of the inlet diffuser for the hydrogenation reaction of the heavy raw oil, the flow plate has a Johnson net structure, and the precision of the flow plate is 0.025mm.
As another optimization scheme of the inlet diffuser for the hydrogenation reaction of the heavy raw oil, the width of the upper spoiler or the lower spoiler is 25-40% of the inner diameter of the cylinder body.
As another optimization scheme of the inlet diffuser for the hydrogenation reaction of the heavy raw oil, the distance between the upper spoiler and the lower spoiler is 0.8-2 times the width of the upper spoiler.
In another preferred embodiment of the inlet diffuser for hydrogenation of heavy feedstock, the diameter of the opening at the small diameter end of the bottom of the rectifying plate is 60-70% of the inner diameter of the cylinder.
As another optimization scheme of the inlet diffuser for the hydrogenation reaction of the heavy raw oil, the outer side wall of the oil-gas inlet of the cylinder body is provided with a mounting clamping plate.
As another optimization scheme of the inlet diffuser for the hydrogenation reaction of the heavy raw oil, the edge of the impact plate exceeds the cylinder and is connected with the bottom of the cylinder through at least three connecting pieces, and a side oil-gas channel is formed between every two adjacent connecting pieces.
As another optimization scheme of the inlet diffuser for the hydrogenation reaction of the heavy raw oil, the impact plate comprises a horizontal plate with oil and gas holes distributed on the surface and a cofferdam arranged around the edge of the upper surface of the horizontal plate.
As another optimization scheme of the inlet diffuser for the hydrogenation reaction of the heavy raw oil, the total area of the oil-gas holes accounts for 10-30% of the area of the horizontal plate.
As another optimization scheme of the inlet diffuser for the hydrogenation reaction of the heavy raw oil, the height of the upper surface of the cofferdam high water outlet flat plate is 5-25mm.
As another optimization scheme of the inlet diffuser for the hydrogenation reaction of the heavy raw oil, the oil gas holes are distributed in a plurality of concentric circles with different diameters around the center of the horizontal plate, according to the sequence from inside to outside, the diameter of the oil gas hole close to the outer side is not smaller than that of the oil gas hole close to the inner side in two adjacent circles of oil gas holes, and the diameter of the oil gas hole close to the outermost side is larger than that of the oil gas hole close to the innermost side; the number of oil and gas holes of each circle is gradually increased from inside to outside and is uniformly distributed along the circle.
As another optimization scheme of the inlet diffuser for the hydrogenation reaction of the heavy raw oil, the oil-gas holes are distributed in 6 circles of concentric circles around the center of the horizontal plate, the diameters of the two innermost circles of oil-gas holes are equal, and the diameters of the oil-gas holes are gradually increased from the second circle of the inner layer to the outside.
A heavy raw oil hydrogenation reactor is characterized in that any one of the inlet diffusers is arranged at the top of a reactor shell.
The heavy raw oil in the present invention means that the density is more than 720kg/m 3 Viscosity > 350mm 2 S (100 ℃), a gum content > 12%.
The working principle of the invention is as follows: in a fixed bed hydrogenation reactor, hydrogen and raw oil are mixed and flow in parallel to enter the reactor, heavy oil has higher density and obviously layered flow is generated at the elbow section of the inlet of the reactor in the hydrogenation reaction, the heavy oil and the hydrogen have large density difference with the hydrogen, the hydrogen is arranged below the liquid phase, so that the inlet has serious bias flow, the fluid with single-side bias flow is corrected twice through the two layers of spoilers and the rectifying plate in the inlet diffuser cylinder body of the invention, and then the fluid is diffused and distributed on the impact disc, and the inner diameters of the two layers of spoilers and the rectifying plate are gradually reduced, and the Johnson net structure of the last layer of rectifying plate has good correction effect on the bias flow. The cofferdam on the impact disc forms a liquid level with a certain thickness, so that the bias current caused by the substandard installation levelness is avoided. The impact plate adopts a flat plate structure, is different from the existing umbrella-shaped structure (a structure with a small top and a large bottom), because the umbrella-shaped structure has a good diffusion effect on low-viscosity fluid, the high-viscosity fluid has strong adhesive force, and is easy to form a dispersion condition consistent with the umbrella plate structure, and the flat plate structure realizes a good diffusion effect on the high-viscosity fluid by matching with a proper hole through impact diffusion.
Compared with the existing inlet diffuser, the invention has the following beneficial effects:
1) According to the inlet diffuser, the two layers of spoilers and the two layers of the rectifying plates are arranged, so that fluid with one-side bias flow is corrected twice and then is subjected to diffusion distribution on the impact disc, a good correction effect is achieved on the bias flow, and the dispersibility is better;
2) The invention has simple structure, can reduce cost and pressure drop as much as possible, provides good initial distribution, and ensures that the catalyst bed layer in the reactor reacts uniformly and the radial temperature difference is smaller.
Drawings
FIG. 1 is a schematic structural view of the present invention;
FIG. 2 is a top view of the inside of the cartridge;
FIG. 3 is a schematic top view of the impingement plate;
FIG. 4 is a schematic view of the radial distribution of liquid in a comparative experiment;
reference numerals: 1. the device comprises a cylinder body, 101, an upper spoiler, 102, a lower spoiler, 103, a rectifying plate, 104, an installation clamping plate, 2, an impact plate, 201, a connecting piece, 202, a side oil-gas channel, 203, a horizontal plate, 204, oil-gas holes, 205 and a cofferdam; A. curve of experimental example, curve of comparative example, B.
Detailed Description
The technical solution of the present invention will be further described in detail with reference to the following embodiments, and the parts of the present invention not illustrated in the following embodiments are understood to be the techniques known or to be known to those skilled in the art, such as the installation of the inlet diffuser and the reactor, the connection of the inlet diffuser and the inlet line, and the structure of the johnson net.
Example 1
An inlet diffuser for hydrogenation reaction of heavy raw oil, as shown in fig. 1 and 2, comprises a cylinder 1 and an impact plate 2 arranged below an oil-gas outlet of the cylinder 1, wherein an installation clamping plate 104 is arranged on the outer side wall of the oil-gas inlet of the cylinder 1, an upper spoiler 101, a lower spoiler 102 and a rectifying plate 103 are sequentially arranged in the cylinder 1 along the oil-gas flowing direction (from top to bottom), the upper spoiler 101 and the lower spoiler 102 are all in a certain distance, wherein the upper spoiler 101 and the lower spoiler 102 are annular plates horizontally arranged in the cylinder 1, the outer side wall of the annular plates is fixed with the cylinder 1, an inner ring forms an oil-gas channel, the rectifying plate 103 is in the shape of an inverted cone with a small-diameter end opening at the bottom, slits are densely distributed on the surface of the rectifying plate, the slits are slits with a length, the top diameter of the rectifying plate 103 is larger than the bottom diameter, and the top is fixedly connected with the inner wall of the cylinder 1.
The above is a basic embodiment of the present invention, and further improvements, optimizations and limitations can be made on the above basis, so as to obtain the following embodiments:
example 2
The present embodiment is to optimize the structure of the flow plate 103 based on embodiment 1, and the main structure thereof is the same as that of embodiment 1, and the optimized solution is as follows: as shown in fig. 1, the diameter of the bottom opening of the current plate 103 is smaller than the diameters of the inner rings of the upper spoiler 101 and the lower spoiler 102, and the diameter of the inner ring of the upper spoiler 101 is not smaller than the diameter of the inner ring of the lower spoiler 102, i.e. the diameter of the inner ring of the upper spoiler 101 can be equal to the diameter of the inner ring of the lower spoiler 102, or can be larger than the diameter of the inner ring of the lower spoiler 102, preferably larger than the diameter of the inner ring of the lower spoiler 102 (i.e. the width of the upper spoiler 101 is smaller than the width of the lower spoiler 102);
the included angle between the generatrix of the rectifying plate 103 and the inner wall of the cylinder 1 is generally 40-60 degrees, preferably 45 degrees;
the diameter of the opening of the small-diameter end at the bottom of the rectifying plate 103 is generally 60-70% of the inner diameter of the cylinder body 1;
the rectifying plate 103 is preferably of a Johnson mesh structure and has an accuracy of 0.025mm.
Example 3
In this embodiment, the upper spoiler 101 and the lower spoiler 102 are optimized on the basis of embodiment 1, the main structure of the embodiment is the same as that of embodiment 1, and the optimized scheme is as follows: as shown in FIG. 2, the width of the upper spoiler 101 or the lower spoiler 102 is generally 25 to 40% of the inner diameter of the cylinder 1, and the distance between the upper spoiler 101 and the lower spoiler 102 is generally 0.8 to 2 times the width of the upper spoiler 101.
Example 4
The present embodiment is an optimization of the impact plate 2 based on embodiment 1, the main structure of which is the same as that of embodiment 1, and the optimization scheme is as follows: as shown in fig. 1 and 3, the impact plate 2 is also circular, and has a diameter larger than that of the barrel 1, so that the edge of the impact plate exceeds the barrel 1 and is connected with the bottom of the barrel 1 through at least three connecting pieces 201, four connecting pieces 201 are shown in the figure, and a side oil and gas channel 202 is formed between the adjacent connecting pieces 201;
the impact plate 2 comprises a horizontal plate 203 with oil and gas holes 204 distributed on the surface and a cofferdam 205 arranged around the edge of the upper surface of the horizontal plate 203; the oil gas holes 204 can be matched with the oil gas channels 202 on the side surface, so that oil gas is uniformly distributed;
the total area of the oil and gas holes 204 generally accounts for 10-30% of the area of the horizontal plate 203;
the height of the cofferdam 205 higher than the upper surface of the horizontal plate 203 is 5-25mm, the cofferdam 205 forms a liquid level with a certain thickness, and the bias current caused by the substandard installation levelness is avoided.
Example 5
In the present embodiment, the oil-air hole 204 in the impact plate 2 is optimized on the basis of embodiment 4, the main structure of the embodiment is the same as that of embodiment 4, and the optimized scheme is as follows: as shown in fig. 3, the oil and gas holes 204 are distributed around the center of the horizontal plate 203 in a plurality of concentric circles with different diameters, that is, a plurality of circles with different diameters concentric with the horizontal plate 203 are drawn on the circular horizontal plate 203 in advance, and the oil and gas holes 204 are uniformly formed on each circle, so that a plurality of circles of concentric circles formed by the oil and gas holes 204 are formed; according to the sequence from inside to outside, in two adjacent circles of oil and gas holes 204, the diameter of the oil and gas hole 204 close to the outer side is not smaller than that of the oil and gas hole 204 close to the inner side, and the diameter of the oil and gas hole 204 in the outermost circle is larger than that of the oil and gas hole 204 in the innermost circle; the number of the oil and gas holes 204 in each circle is gradually increased from inside to outside and is evenly distributed along the circle.
In this embodiment, it is preferable that the oil and gas holes 204 are distributed around the center of the horizontal plate 203 in 6 circles concentrically, the diameters of the innermost two circles of oil and gas holes 204 are equal, and the diameter of each circle of oil and gas holes 204 gradually increases from the second circle of the inner layer to the outside.
Example 6
A heavy raw oil hydrogenation reactor, wherein the top of the reactor shell is provided with an inlet diffuser as in any one of the embodiments 1-5.
In order to verify the uniform distribution effect of the invention on heavy oil, the following comparative experiment is carried out:
examples of the experiments
The inlet diffuser structure of the experimental example is shown in fig. 1, and comprises a cylinder 1 and an impact plate 2, wherein an installation clamping plate 104 is arranged on the outer side wall of an oil gas inlet of the cylinder 1, an upper spoiler 101, a lower spoiler 102 and a rectifying plate 103 are sequentially arranged in the cylinder 1 along the oil gas flowing direction (from top to bottom), the impact plate 2 is connected with the bottom of the cylinder 1 through four connecting pieces 201, and the impact plate 2 comprises a horizontal plate 203 with oil gas holes 204 distributed on the surface and a cofferdam 205 arranged around the edge of the upper surface of the horizontal plate 203;
wherein the diameter of the mounting clamping plate 104 is 960mm, the plate thickness is 8mm, and the mounting clamping plate is welded with the upper end of the cylinder 1; the height of the cylinder body 1 is 1325mm, the outer diameter is 970mm, and the wall thickness is 8mm;
the upper spoiler 101 is 500mm away from the upper end surface of the cylinder 1, the inner diameter is 680mm, the thickness is 8mm, the distance from the lower spoiler 102 to the upper spoiler 101 is 300mm, the inner diameter is 660mm, and the thickness is 8mm;
the rectifying plate 103 is in an inverted cone shape, the diameter of an opening at the bottom is 600mm, the included angle between the rectifying plate and the cylinder body 1 is 45 ℃, a Johnson net structure is adopted, the precision is 0.025mm, the large-diameter end is arranged above, and the small-diameter end is arranged below to form an opening;
the number of the connecting pieces 201 is four, the height is 180mm, the thickness is 10mm, the connecting pieces are uniformly distributed in a centering way, the upper ends of the connecting pieces are connected with the cylinder body 1, and the lower ends of the connecting pieces are connected with the impact plate 2;
the diameter of a horizontal plate 203 is 990mm, the thickness of the horizontal plate is 8mm, oil and gas holes 204 are formed in the horizontal plate, 6 first circle oil and gas holes 204 with the diameter of 30mm are uniformly distributed in the diameter of 150mm, 8 second circle oil and gas holes 204 with the diameter of 30mm are uniformly distributed in the diameter of 250mm, 10 third circle oil and gas holes 204 with the diameter of 40mm are uniformly distributed in the diameter of 350mm, 12 fourth circle oil and gas holes 204 with the diameter of 50mm are uniformly distributed in the diameter of 500mm, 14 fifth circle oil and gas holes 204 with the diameter of 55mm are uniformly distributed in the diameter of 750mm, and 16 sixth circle oil and gas holes 204 with the diameter of 60mm are uniformly distributed in the diameter of 850 mm;
the cofferdam 205 is 18mm high and 8mm thick.
Comparative example
The inlet diffuser used in the comparative example is a patent publication with the patent number 200820070429.8, which is generally used for inlet diffusion of light oil hydrogenation.
Two kinds of inlet diffusers of the experimental example and the comparative example were installed on the reactor, respectively, the reactor diameter was 4200mm, the throughput was 285kg/h, and the properties of the heavy feed oil were: density 784.21kg m 3 Kinematic viscosity 632.1 (100 ℃ C.)/mm 2 ·s -1 Surface tension of 6.53mN · m -1 The gum content is 14.8%;
under the condition of the same process parameters, the heavy raw oil is introduced into the reactors of the experimental example and the comparative example, and the radial distribution condition of the liquid 200mm below the inlet diffuser is detected as shown in the attached figure 4;
three points are taken at different positions on the catalyst bed layer 200mm below the inlet diffuser, the temperature is respectively detected, the maximum temperature difference is calculated to evaluate the uniformity of the catalyst bed layer reaction, and the detection results are shown in the following table:
| temperature measuring point I | Temperature measuring point two | Temperature measuring point three | Maximum temperature difference | |
| Comparative example | 363.2℃ | 368.1℃ | 365.2℃ | 4.9℃ |
| Examples of the experiments | 369.2℃ | 371.5℃ | 370.5℃ | 2.3℃ |
As can be seen from figure 4 and the attached table, when the experimental example is used in a hydrogenation reactor, the problem of uneven dispersion of the umbrella plate structure to high-viscosity fluid can be solved, the dispersion is uniform on a 200mm interface below the umbrella plate structure, and good initial distribution is provided for a lower bed layer; the catalyst bed layer has uniform reaction and smaller radial temperature difference.
Claims (15)
1. The utility model provides a heavy raw oil hydrogenation is with entry diffuser, includes barrel (1) and striking plate (2) of setting in barrel (1) oil gas export below, its characterized in that: the oil gas well-sealed oil well is characterized in that an upper spoiler (101), a lower spoiler (102) and a rectifying plate (103) are sequentially arranged in the cylinder body (1) along the oil gas flowing direction, wherein the upper spoiler (101) and the lower spoiler (102) are annular plates horizontally arranged in the cylinder body (1), the rectifying plate (103) is in the shape of an inverted cone with a small-diameter end at the bottom and an opening, and slits are densely distributed in the surface of the rectifying plate.
2. The inlet diffuser for hydrogenation reaction of heavy raw oil according to claim 1, wherein: the diameter of an opening at the bottom end of the rectifying plate (103) is smaller than the diameters of the inner rings of the upper spoiler (101) and the lower spoiler (102), and the diameter of the inner ring of the upper spoiler (101) is not smaller than the diameter of the inner ring of the lower spoiler (102).
3. The inlet diffuser for hydrogenation reaction of heavy raw oil according to claim 1, wherein: the included angle between the bus of the rectifying plate (103) and the inner wall of the barrel (1) is 40-60 degrees.
4. The inlet diffuser for hydrogenation reaction of heavy raw oil according to claim 1, wherein: the rectifying plate (103) is of a Johnson mesh structure, and the precision of the rectifying plate is 0.025mm.
5. The inlet diffuser for hydrogenation reaction of heavy raw oil according to claim 1, wherein: the width of the upper spoiler (101) or the lower spoiler (102) is 25-40% of the inner diameter of the cylinder body (1).
6. The inlet diffuser for hydrogenation reaction of heavy raw oil according to claim 1, wherein: the distance between the upper spoiler (101) and the lower spoiler (102) is 0.8-2 times of the width of the upper spoiler (101).
7. The inlet diffuser for hydrogenation reaction of heavy raw oil according to claim 1, characterized in that: the diameter of the opening of the small-diameter end at the bottom of the rectifying plate (103) is 60-70% of the inner diameter of the cylinder (1).
8. The inlet diffuser for hydrogenation reaction of heavy raw oil according to claim 1, wherein: the outer side wall of the oil gas inlet of the cylinder body (1) is provided with a mounting clamping plate (104).
9. The inlet diffuser for hydrogenation reaction of heavy raw oil according to claim 1, wherein: the edge of the impact plate (2) exceeds the cylinder body (1) and is connected with the bottom of the cylinder body (1) through at least three connecting pieces (201), and a side oil gas channel (202) is formed between every two adjacent connecting pieces (201).
10. The inlet diffuser for hydrogenation reaction of heavy raw oil according to claim 1, wherein: the impact plate (2) comprises a horizontal plate (203) with oil and gas holes (204) distributed on the surface and a cofferdam (205) arranged around the edge of the upper surface of the horizontal plate (203).
11. The inlet diffuser for hydrogenation reaction of heavy raw oil according to claim 10, characterized in that: the total area of the oil and gas holes (204) accounts for 10-30% of the area of the horizontal plate (203).
12. The inlet diffuser for hydrogenation reaction of heavy raw oil according to claim 10, characterized in that: the height of the cofferdam (205) above the upper surface of the water outlet flat plate (203) is 5-25mm.
13. The inlet diffuser for hydrogenation reaction of heavy raw oil according to claim 10, characterized in that: the oil and gas holes (204) are distributed around the center of the horizontal plate (203) in a plurality of concentric circles with different diameters, according to the sequence from inside to outside, in two adjacent circles of oil and gas holes (204), the diameter of the oil and gas hole (204) close to the outer side is not smaller than that of the oil and gas hole (204) close to the inner side, and the diameter of the oil and gas hole (204) in the circle at the outermost side is larger than that of the oil and gas hole (204) in the circle at the innermost side; the number of the oil and gas holes (204) of each circle is gradually increased from inside to outside and is evenly distributed along the circle.
14. The inlet diffuser for hydrogenation reaction of heavy raw oil according to claim 13, characterized in that: oil gas hole (204) are 6 rings of concentric circles around the center of horizontal plate (203) and distribute, and the diameter of two rings of oil gas hole (204) at the innermost equals, and outside the inlayer second circle, the diameter of each ring of oil gas hole (204) crescent.
15. A heavy raw oil hydrogenation reactor is characterized in that: an inlet diffuser as claimed in any one of claims 1 to 14 is provided at the top of the reactor shell.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211363705.0A CN115738905B (en) | 2022-11-02 | 2022-11-02 | Inlet diffuser for heavy raw oil hydrogenation reaction and hydrogenation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211363705.0A CN115738905B (en) | 2022-11-02 | 2022-11-02 | Inlet diffuser for heavy raw oil hydrogenation reaction and hydrogenation reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115738905A true CN115738905A (en) | 2023-03-07 |
| CN115738905B CN115738905B (en) | 2024-08-13 |
Family
ID=85355478
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211363705.0A Active CN115738905B (en) | 2022-11-02 | 2022-11-02 | Inlet diffuser for heavy raw oil hydrogenation reaction and hydrogenation reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115738905B (en) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3469950A (en) * | 1963-11-21 | 1969-09-30 | British Petroleum Co | Fixed-bed catalytic operations |
| DE4108516A1 (en) * | 1990-03-16 | 1991-09-19 | Hitachi Ltd | HIGH-SPEED SEEDING DEVICE AND HIGH-SPEED SEEDING METHOD |
| JPH07136492A (en) * | 1993-11-19 | 1995-05-30 | Hitachi Ltd | Fluid supply mechanism and filter desalting device |
| CN205435679U (en) * | 2016-03-18 | 2016-08-10 | 北京安耐吉能源工程技术有限公司 | Entry diffuser and hydrogenation ware |
| CN106237936A (en) * | 2016-08-19 | 2016-12-21 | 兰州兰石集团有限公司 | Gas-liquid cocurrent flow inlet diffuser |
| CN107904144A (en) * | 2017-12-06 | 2018-04-13 | 山西农业大学 | Microalgae column reactor is aerated disturbing flow device |
| CN112705119A (en) * | 2019-10-25 | 2021-04-27 | 中国石油化工股份有限公司 | Heavy oil hydrogenation reactor and hydrogenation method |
-
2022
- 2022-11-02 CN CN202211363705.0A patent/CN115738905B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3469950A (en) * | 1963-11-21 | 1969-09-30 | British Petroleum Co | Fixed-bed catalytic operations |
| DE4108516A1 (en) * | 1990-03-16 | 1991-09-19 | Hitachi Ltd | HIGH-SPEED SEEDING DEVICE AND HIGH-SPEED SEEDING METHOD |
| JPH07136492A (en) * | 1993-11-19 | 1995-05-30 | Hitachi Ltd | Fluid supply mechanism and filter desalting device |
| CN205435679U (en) * | 2016-03-18 | 2016-08-10 | 北京安耐吉能源工程技术有限公司 | Entry diffuser and hydrogenation ware |
| CN106237936A (en) * | 2016-08-19 | 2016-12-21 | 兰州兰石集团有限公司 | Gas-liquid cocurrent flow inlet diffuser |
| CN107904144A (en) * | 2017-12-06 | 2018-04-13 | 山西农业大学 | Microalgae column reactor is aerated disturbing flow device |
| CN112705119A (en) * | 2019-10-25 | 2021-04-27 | 中国石油化工股份有限公司 | Heavy oil hydrogenation reactor and hydrogenation method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115738905B (en) | 2024-08-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102596386B (en) | Fluidized-bed reactor and hydrotreating method thereof | |
| CN105694959A (en) | Jet-type internal circulation flow reactor for heavy oil hydrocracking | |
| CN115738905B (en) | Inlet diffuser for heavy raw oil hydrogenation reaction and hydrogenation reactor | |
| CN111690433B (en) | FCC feedstock liquid phase hydroprocessing system and method | |
| CN109722281B (en) | Fluidized bed reactor with multiple catalysts for internal circulation and hydrogenation method thereof | |
| US20240336853A1 (en) | Heavy oil hydrogenation reaction system and heavy oil hydrogenation method | |
| CN111298722A (en) | Hydrogenation reactor and hydrogenation method for hydrocarbon raw material | |
| CN219571911U (en) | Burner plate of acetylene cracking furnace | |
| CN108067169B (en) | Ebullated bed reactor | |
| CN114437809B (en) | Liquid phase hydrogenation device and liquid phase hydrogenation method | |
| CN114479925B (en) | Heavy oil hydrogenation reaction system and heavy oil hydrogenation method | |
| CN114425280B (en) | Feeding distributor and reactor | |
| CN113122316B (en) | Method for prolonging operation period of heavy oil hydrogenation device | |
| CN112275225B (en) | Radial moving bed reaction system and flow-solid reaction method | |
| CN112708447B (en) | A Riser Reactor with Reduced Backmixing in the Sidewall Region | |
| CN219297623U (en) | Nitriding furnace with atmosphere homogenizing device | |
| CN115785995B (en) | Inferior diesel oil hydrotreating method and device | |
| CN115785994B (en) | Wax oil hydrogenation method and device | |
| CN114806631B (en) | Method for prolonging operation period of fixed bed heavy oil hydrogenation device | |
| CN222956359U (en) | Tubular fixed bed reactor | |
| CN212819922U (en) | Catalytic reforming reactor | |
| CN110003936B (en) | Feeding method and device for rotational flow cushion layer of hydrogenation reactor | |
| CN116064146B (en) | One-stage series hydrocracking method | |
| CN119425529A (en) | Gas-liquid distributor and upward reactor | |
| CN117467472B (en) | A fluidized bed-fixed bed combined hydroprocessing process and processing system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |