CN209923264U - Up-flow liquid phase hydrogenation reactor - Google Patents
Up-flow liquid phase hydrogenation reactor Download PDFInfo
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- CN209923264U CN209923264U CN201920547389.XU CN201920547389U CN209923264U CN 209923264 U CN209923264 U CN 209923264U CN 201920547389 U CN201920547389 U CN 201920547389U CN 209923264 U CN209923264 U CN 209923264U
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 117
- 239000007791 liquid phase Substances 0.000 title claims abstract description 27
- 239000003054 catalyst Substances 0.000 claims abstract description 103
- 229910052751 metal Inorganic materials 0.000 claims abstract description 86
- 239000002184 metal Substances 0.000 claims abstract description 86
- 239000000919 ceramic Substances 0.000 claims abstract description 73
- 239000002245 particle Substances 0.000 claims abstract description 35
- 239000003795 chemical substances by application Substances 0.000 claims description 24
- 235000005770 birds nest Nutrition 0.000 claims description 15
- 235000005765 wild carrot Nutrition 0.000 claims description 15
- 239000011148 porous material Substances 0.000 claims description 12
- 239000001257 hydrogen Substances 0.000 abstract description 22
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 22
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 20
- 239000012071 phase Substances 0.000 abstract description 10
- 239000007789 gas Substances 0.000 abstract description 7
- 239000000463 material Substances 0.000 abstract description 6
- 230000000694 effects Effects 0.000 abstract description 5
- 230000003139 buffering effect Effects 0.000 abstract description 2
- 239000006185 dispersion Substances 0.000 abstract description 2
- 238000001556 precipitation Methods 0.000 abstract 1
- 229910052573 porcelain Inorganic materials 0.000 description 17
- 238000006243 chemical reaction Methods 0.000 description 10
- 239000007788 liquid Substances 0.000 description 10
- 125000003118 aryl group Chemical group 0.000 description 7
- 238000000034 method Methods 0.000 description 7
- 238000007599 discharging Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 150000001336 alkenes Chemical class 0.000 description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 229910000480 nickel oxide Inorganic materials 0.000 description 3
- 229910000510 noble metal Inorganic materials 0.000 description 3
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 description 3
- 230000008439 repair process Effects 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 230000005465 channeling Effects 0.000 description 2
- 238000006298 dechlorination reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000007792 gaseous phase Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- 229910018879 Pt—Pd Inorganic materials 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000007809 chemical reaction catalyst Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000005235 decoking Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a hydrogenation ware of upflow liquid phase hydrogenation, it includes: a feed inlet; a discharge port; a catalyst bed layer; the first metal layer is arranged above the catalyst bed layer, the first metal layer is a metal net and/or a grid, and the aperture of the first metal layer is smaller than the particle size of the catalyst in the catalyst bed layer; the upper ceramic ball layers are arranged above the first metal layer, and the particle size of each upper ceramic ball layer is gradually increased from bottom to top; the second metal layer is arranged below the catalyst bed layer and is a metal net and/or a grid; the lower ceramic ball layers are arranged below the second metal layer, and the particle size of each lower ceramic ball layer is gradually increased from top to bottom; and the baffling layer is arranged between the lower ceramic ball layers and the feed inlet. The utility model is provided with a plurality of ceramic ball layers, which can redistribute the material flow and avoid the gas phase precipitation; set up the baffling layer and can play the effect of dispersion, dissolved hydrogen and buffering to the material, prolong the utility model discloses a life.
Description
Technical Field
The utility model relates to an up-flow liquid phase hydrogenation's hydrogenation ware.
Background
For a traditional fixed bed hydrogenation reactor, gas, liquid and solid phases coexist during hydrogenation reaction, the gas phase is the vapor of hydrogen and hydrocarbon raw materials, the liquid phase is unvaporized hydrocarbon raw materials, and the solid phase is a catalyst. The two phases, gas and liquid, are passed in trickle flow through the catalyst bed and are therefore also referred to as trickle bed reactors. The reactions of desulfurization, denitrification and the like of the conventional trickle bed hydrogenation reactor mainly use hydrogen mass transfer, namely the speed of hydrogen diffusing from a gas phase and dissolving into oil is the control step of the whole hydrogenation reaction.
The liquid phase hydrogenation technology is a novel hydrogenation technology. The liquid phase hydrogenation process is characterized in that the influence of hydrogen mass transfer is eliminated, the hydrogenation reaction is carried out in a dynamic control area, namely, the hydrogen is dissolved in the raw oil to meet the hydrogen required by the hydrogenation reaction, the pure liquid phase reaction is carried out in a reactor, the influence of mass transfer of the hydrogen from a gas phase to a liquid phase can be eliminated, sufficient hydrogen is dissolved through liquid circulation to meet the requirement of the hydrogenation reaction, and the investment of equipment such as a recycle hydrogen compressor, a high-pressure separator and the like is saved. Compared with the traditional trickle bed process, the liquid phase hydrogenation process flow is not provided with a hydrogen circulation system and a gas-liquid separation system, so that the investment cost is greatly reduced, a liquid phase circulation system and a static mixer of hydrogen and oil are added, the hydrogen is completely dissolved in the feed, and the material in the reactor exists in a pure liquid phase state.
The main internal components of the traditional fixed bed hydrogenation reactor are an inlet diffuser, a gas-liquid distribution disc, a catalyst bed layer support, a cold hydrogen tank, an outlet collector and the like, wherein the internal components directly related to the use efficiency of the catalyst are the gas-liquid distribution disc and the cold hydrogen tank. In order to adapt to liquid phase hydrogenation, a person skilled in the art develops a new reactor on the basis of the existing fixed bed hydrogenation reactor, but the reactors are still provided with a large number of internal components, so that the cost of the hydrogenation reactor is high, the maintenance and the repair are difficult, and the internal components occupy a large amount of internal space, so that the space of a catalyst bed is insufficient.
For example, CN 104178217 a discloses a liquid phase hydrogenation method and a reactor thereof. The reactor comprises a reactor cylinder, a mixing dissolver, a stripping distributor, a catalyst bed layer, a reactor outlet and a reactor inlet, wherein the mixing dissolver, the stripping distributor and the catalyst bed layer are arranged in the reactor cylinder. The upper part of the reactor is also provided with a separation tray or packing. The reactor is still provided with internal components such as a mixing dissolver, a stripping distributor, a separation tower tray and the like, so that the hydrogenation reactor is high in cost and difficult to maintain and repair, and the internal components occupy a large amount of internal space, so that the space of a catalyst bed layer is insufficient.
SUMMERY OF THE UTILITY MODEL
To the deficiency of the prior art, the utility model provides an upflow liquid phase hydrogenation reactor. The hydrogenation reactor avoids the phenomena of bias flow, channeling and the like under the condition of not arranging internal components such as an inlet diffuser, an outlet collector, a mixing dissolver, a stripping distributor and the like, can also avoid the back mixing phenomenon between the upper part of a catalyst bed layer and a ceramic ball, and solves the problem of leakage of the hydrogenation catalyst.
In order to achieve the above object, the present invention provides an upflow liquid phase hydrogenation reactor, which comprises: the feeding hole is arranged at the bottom of the hydrogenation reactor; the discharge hole is arranged at the top of the hydrogenation reactor; a catalyst bed disposed within the hydrogenation reactor; the first metal layer is arranged above the catalyst bed layer, the first metal layer is a metal net and/or a metal grid, and the aperture of the first metal layer is smaller than the particle size of the catalyst in the catalyst bed layer; the upper ceramic ball layers are arranged above the first metal layer, and the particle size of each upper ceramic ball layer is gradually increased from bottom to top; the second metal layer is arranged below the catalyst bed layer, and the second metal layer is a metal net and/or a metal grid; the lower ceramic ball layers are arranged below the second metal layer, and the particle size of each lower ceramic ball layer is gradually increased from top to bottom; and the baffling layer is arranged between the lower ceramic ball layers and the feed inlet.
Further, in the above technical scheme, the wall body of the hydrogenation reactor is provided with upper agent discharging ports at the positions of the plurality of upper ceramic ball layers.
Further, in the above technical scheme, the wall body of the hydrogenation reactor is provided with a lower agent discharging port at the positions of the plurality of lower ceramic ball layers.
Further, in the above technical scheme, the wall body of the hydrogenation reactor is provided with a middle agent discharging port at the catalyst bed layer.
Further, in the above technical solution, the hydrogenation reactor further includes: and the support grating is arranged between the lower ceramic ball layers and the baffling layer.
Further, in the above technical solution, the hydrogenation reactor further includes: and the bird nest propping agent is arranged between the lower ceramic ball layers and the support grid.
Further, in the above technical solution, the hydrogenation reactor further includes: and the third metal layer is arranged between the support grid and the bird nest propping agent, and the third metal layer is a metal net and/or a metal grid, and the aperture of the third metal layer is smaller than the particle size of the bird nest propping agent.
Further, in the above technical scheme, the plurality of upper ceramic ball layers are three layers.
Further, in the above technical scheme, the particle diameters of the three upper ceramic ball layers are respectively 4-7 mm, 10-14 mm and 16-20 mm from bottom to top, and the ratio of the height of the three upper ceramic ball layers to the height of the catalyst bed layer is (0.15-3.0): 10. (0.15-3.0): 10. (0.15-3.0): 10.
further, in the above technical scheme, the plurality of lower ceramic ball layers are three layers.
Further, in the above technical scheme, the particle diameters of the three lower ceramic ball layers are respectively 4-7 mm, 10-14 mm and 16-20 mm from top to bottom, and the ratio of the height of the three lower ceramic ball layers to the height of the catalyst bed layer is (0.15-3.0): 10. (0.15-3.0): 10. (0.15-3.0): 10.
further, in the above technical solution, the aperture of the first metal layer is smaller than the particle size of the plurality of upper ceramic ball layers; the aperture of the second metal layer is smaller than the particle size of the catalyst in the catalyst bed layer, and the aperture of the second metal layer is smaller than the particle sizes of the lower ceramic ball layers.
Furthermore, in the above technical solution, the aperture of the first metal layer is 12-16 meshes, and the aperture of the second metal layer is 12-16 meshes.
Further, in the technical scheme, the particle size of the catalyst in the catalyst bed layer is smaller than 12 meshes.
Further, in the above technical solution, the first metal layer is disposed on the catalyst bed.
Compared with the prior art, the utility model discloses following beneficial effect has:
1. the utility model discloses a hydrogenation reactor, catalyst bed top, below all are provided with multilayer porcelain ball, but the redistribution commodity circulation, the commodity circulation in making the hydrogenation reactor distributes evenly, make the hydrogen disperse phase difficult to separate out from the liquid phase simultaneously, avoid appearing hydrogen and appear local gathering, improve the homogeneity of gas, liquid double-phase in the flow process, especially a plurality of ceramic ball layers, can avoid gaseous phase to separate out, thereby the commodity circulation that is favorable to after the hydrogenation is whole to be carried next device smoothly, thereby avoided current liquid phase hydrogenation because gaseous phase separates out, need complicated reactor internals and instrument to control the problem of liquid level; a metal net and/or a metal grid are/is arranged between the ceramic ball layer and the catalyst bed layer, the aperture of the first metal layer is smaller than the particle size of the catalyst in the catalyst bed layer, so that the problem that the catalyst in the catalyst bed layer is mixed with the ceramic ball layer and then the catalyst and the ceramic ball are mixed back is avoided, and the problem of leakage of the hydrogenation catalyst is also thoroughly solved; the baffling layer is arranged to enable feeding to be more uniform dispersedly, hydrogen can be better dissolved in raw oil, and the baffling channel can play a role in buffering, so that a catalyst bed layer is prevented from shifting, and the service life is prolonged.
2. The utility model discloses a hydrogenation ware no longer sets up internals such as entry diffuser, export collector, mixed dissolvent, strip distributor, still reaches very good liquid phase hydrogenation effect to reduce the investment cost of reactor by a wide margin, easy to maintain and repair saves the internals space moreover, can increase the space of catalyst bed, realizes higher liquid phase hydrogenation effect.
3. The utility model discloses an among the hydrogenation ware, catalyst bed layer below is equipped with the support grid, and the structure is more firm.
4. Meanwhile, the hydrogenation reactor is provided with an upper agent discharging port, a middle agent discharging port and a lower agent discharging port in a matching way, so that the ceramic balls and the catalyst are respectively discharged, and the subsequent separation operation of the ceramic balls and the catalyst is avoided.
5. The utility model discloses hydrogenation reactor flow is simple, and equipment investment is lower, and maintenance cost is lower, can be used to processes such as reformate hydrogenation de-olefine, arene raffinate oil hydrogenation de-olefine and alkylate oil hydrogenation dechlorination.
The foregoing description is only an overview of the technical solutions of the present invention, and in order to make the technical means of the present invention more clearly understood and to make the technical means more comprehensible, and to make the above and other objects, technical features, and advantages of the present invention easier to understand, one or more preferred embodiments are listed below, and the following detailed description is given with reference to the accompanying drawings.
Drawings
Fig. 1 is a schematic diagram of a hydrogenation reactor according to one or more embodiments of the present invention.
Description of the main reference numerals:
1-a hydrogenation reactor, 11-a feed inlet, 12-a discharge outlet, 20-a catalyst bed layer, 31-a first metal layer, 32-a second metal layer, 41-a first upper ceramic ball layer, 42-a second upper ceramic ball layer, 43-a third upper ceramic ball layer, 51-a first lower ceramic ball layer, 52-a second lower ceramic ball layer and 53-a third lower ceramic ball layer. 60-bird nest proppant, 70-support grid, 80-baffling layer and 81-baffle plate.
Detailed Description
The following detailed description of the present invention is provided in conjunction with the accompanying drawings, but it should be understood that the scope of the present invention is not limited by the following detailed description.
Throughout the specification and claims, unless explicitly stated otherwise, the word "comprise", or variations such as "comprises" or "comprising", will be understood to imply the inclusion of a stated element or component but not the exclusion of any other element or component.
Spatially relative terms, such as "below," "lower," "upper," "above," "upper," and the like, may be used herein for ease of description to describe one element or feature's relationship to another element or feature in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations of the object in use or operation in addition to the orientation depicted in the figures. For example, if the items in the figures are turned over, elements described as "below" or "beneath" other elements or features would then be oriented "above" the elements or features. Thus, the exemplary term "below" can encompass both an orientation of below and above. The article may be otherwise oriented (rotated 90 degrees or at other orientations) and the spatially relative terms used herein should be interpreted accordingly.
In this document, the terms "first", "second", etc. are used to distinguish two different elements or portions, and are not used to define a particular position or relative relationship. In other words, the terms "first," "second," and the like may also be interchanged with one another in some embodiments.
As shown in fig. 1, the present invention provides a hydrogenation reactor 1 for upflow liquid phase hydrogenation, the hydrogenation reactor 1 is provided with a feed inlet 11 at the bottom thereof and a discharge outlet 12 at the top thereof, a first metal layer 31 (metal mesh and/or metal grid), a plurality of upper ceramic ball layers with gradually increasing particle sizes, and a second metal layer 32 (metal mesh and/or metal grid), a plurality of lower ceramic ball layers with gradually increasing particle sizes, and a baffle layer 80 are sequentially disposed above a catalyst bed 20 in the hydrogenation reactor 1 from bottom to top, the first metal layer 31 has a smaller pore size than the catalyst in the catalyst bed 20, for example, when the first metal layer 31 has a 12-16 mesh pore size, the catalyst has a smaller particle size than the 12 mesh size, the second metal layer 32 has a pore size smaller than the catalyst in the catalyst bed 20, for example, the second metal layer 32 has a 12-16 mesh size, and the second metal layer 32 has a smaller pore size, for example, the second metal layer 32 has a 3580-11 mesh size, and a baffle angle, and the baffle angle of the baffle layer is preferably equal to the shape of the baffle plate, and the baffle plate is not limited by the practical shape of the metal layer 80, and the baffle plate 11.
The utility model discloses an in one or more embodiments, the wall body of hydrogenation ware 1 is provided with in a plurality of porcelain ball layer departments of going up of catalyst bed 20 top and unloads the agent mouth (not shown in the figure), and a plurality of porcelain ball layer departments of the wall body of hydrogenation ware 1 below catalyst bed 20 are provided with down unloads the agent mouth (not shown in the figure), and the wall body of hydrogenation ware 1 unloads the agent mouth (not shown in the figure) in catalyst bed 20 department is provided with.
In one or more embodiments of the present invention, a support grid 70 is further disposed below the catalyst bed 20, and preferably, a bird nest supporting agent 60 is disposed between the lower ceramic ball layers and the support grid 70. the bird nest supporting agent 60 may be a porous supporting agent, so as to absorb dirt in the hydrogenation feedstock oil and prevent the dirt from affecting the catalyst bed 20. a third metal layer (which is a metal mesh and/or a metal grid, not shown) is further disposed between the support grid 70 and the bird nest supporting agent 60. the pore size of the third metal layer is smaller than that of the bird nest supporting agent 60. the particle size of the bird nest supporting agent 60 is preferably 40-50 mm, and the pore size of the third metal layer is preferably 12-16 mesh. it should be understood that the present invention is not limited thereto, and those skilled in the art can select the particle size of the bird nest supporting agent according to the actual needs of the hydrogenation reactor, the pore size of the third metal layer is smaller than that of the bird nest supporting agent, i.e. the flow stopping layer shown in fig. 80, the flow stopping layer, the present invention is not limited to a distance of 3580 mm, and the present invention can be connected to a distance of a honeycomb supporting grid, and can be understood by a distance of 3580 mm.
In one or more embodiments of the present invention, the first metal layer 31 is placed on the catalyst bed 20. After the catalyst bed layer 20 is filled, the first metal layer 31 is directly placed on the upper part of the catalyst bed layer 20 without being connected and fixed with the wall body of the hydrogenation reactor 1, then the ceramic ball layer is filled, and the first metal layer is pressed by the gravity of the ceramic balls, so that the purposes of conveniently filling the catalyst bed layer and flexibly adjusting the height of the catalyst bed layer are achieved. As an alternative embodiment, the first metal layer 31 may be fixed to the wall of the hydrogenation reactor 1 when the catalyst bed 20 has a predetermined catalyst bed height or when the catalyst bed height does not change.
The utility model discloses an in one or more embodiments, a plurality of porcelain ball layers of going up are the three-layer, are porcelain ball layer 42, porcelain ball layer 43 on the third on porcelain ball layer 41, the second respectively for the first, and the particle diameter of porcelain ball layer is 4 ~ 7mm, 10 ~ 14mm, 16 ~ 20mm respectively on the three-layer that makes progress down, and the ratio of height and catalyst bed 20's height is (0.5 ~ 3.0) respectively: 10. (0.5-3.0): 10. (0.5-3.0): 10. it should be understood that the present invention is not limited thereto, and those skilled in the art can determine the height of the catalyst bed layer and the height of the first upper ceramic ball layer 41, the second upper ceramic ball layer 42, and the third upper ceramic ball layer 43 according to the actual requirement of the hydrogenation reactor, and the ceramic ball gravity can press the first metal layer 31. As an alternative embodiment, when the first metal layer 31 is fixed on the wall of the hydrogenation reactor 1, the upper ceramic ball layer no longer generates gravity action on the catalyst bed 20, and then the ceramic balls are filled and the height of the ceramic ball layer is adjusted in a conventional manner, regardless of the above-mentioned proportional relationship between the height of the ceramic ball layer and the height of the catalyst bed.
The utility model discloses an in one or more embodiments, a plurality of porcelain ball layers down are the three-layer, are porcelain ball layer 52 under first porcelain ball layer 51, the second respectively, porcelain ball layer 53 under the third, and the particle diameter on porcelain ball layer is 4 ~ 7mm, 10 ~ 14mm, 16 ~ 20mm respectively under the three-layer from the top down, and the ratio of height and catalyst bed 20's height is (0.5 ~ 3.0) respectively: 10. (0.5-3.0): 10. (0.5-3.0): 10.
the utility model discloses a hydrogenation reactor is applicable to the liquid phase reaction state, and under reaction condition, at least partial raw oil is the liquid phase state, and preferably, raw oil 80 wt% at least keeps the liquid phase state, and further preferably, raw oil 90wt% at least keeps the liquid phase state.
In one or more embodiments of the present invention, the feed inlet 11 of the reaction material is disposed at the bottom of the hydrogenation reactor 1, so that the material enters the hydrogenation reactor 1 from the bottom of the hydrogenation reactor 1Thereby carrying out the hydrogenation reaction in an upflow mode of operation. The conditions of the hydrogenation reaction were as follows: the reaction pressure is 0.5 MPa to 6.0 MPa, preferably 1.2 MPa to 3.0 MPa; the reaction temperature is 100-240 ℃, preferably 140-200 ℃; the liquid hourly space velocity is 1.0 h-1～12.0 h-1Preferably 4.0 h-1～8.0 h-1(ii) a The volume ratio of hydrogen to oil is 20: 1 or less, preferably 2: 1-5: 1. in the utility model, the volume ratio of hydrogen to oil can be obviously reduced compared with the conventional method.
In one or more embodiments of the present invention, the hydrorefining catalyst used may be a commercial hydrorefining catalyst, such as a hydrorefining catalyst using a noble metal or reduced nickel as an active component, and such a catalyst has a high hydrogenation activity and can perform hydrogenation reaction at a relatively low temperature. Preferably, a hydrofining catalyst taking noble metal as an active component is adopted, such as an HDO-18 catalyst developed and produced by the Fushun petrochemical research institute. The noble metal hydrorefining catalyst generally takes alumina as a carrier and Pt and/or Pd as active components, and the content of the active components in the catalyst is not less than 0.1 percent by weight, and is generally 0.1 to 1.5 percent by weight. For the hydrofining catalyst with reduced nickel as an active component, generally, alumina or modified alumina is used as a carrier, nickel oxide is used as an active component (the weight of nickel oxide accounts for 15-70% of the weight of the catalyst, and preferably 25-45%), before use, the catalyst is subjected to reduction activation, and the nickel oxide is converted into a reduced state, so as to improve the hydrogenation activity of the catalyst.
The utility model discloses a hydrogenation ware can be used to reformate hydrogenation de-olefin, arene raffinate oil hydrogenation de-olefin and alkylate oil hydrogenation dechlorination process such as.
The following examples further illustrate the invention.
The catalyst is used as a hydrogenation reaction catalyst for industrial application, and is an HDO-18 hydrogenation catalyst developed and produced by the smooth petrochemical research institute, and the indexes of the physical and chemical properties of the catalyst are shown in Table 1.
TABLE 1 index of physicochemical Properties of the catalyst
| Catalyst numbering | HDO-18 |
| Metal composition | Pt-Pd |
| Physical Properties | |
| Pore volume, mL/g | ≥0.45 |
| Specific surface area, m2/g | ≥170 |
| Compressive strength, N/cm | ≥90 |
| Particle size, mm | 2.0~3.0 |
| Length, mm | 3.0~8.0 |
| Shape of | Cylindrical bar shape |
Example 1
Adopt the utility model discloses a hydrogenation ware 1 in the embodiment, do not set up relevant internals such as entry diffuser, cold hydrogen case, export collector, mixed dissolver, strip distributor in hydrogenation ware 1, but in catalyst bed 20's top, be provided with porcelain ball layer 41 on the first, porcelain ball layer 42 on the second, porcelain ball layer 43 on the third, the particle diameter of porcelain ball layer is 6mm, 13mm, 19mm on the three-layer that makes progress down respectively, highly be 200mm, 290mm respectively, catalyst bed 20 highly is 8100 mm. The catalyst bed layer 20 is provided with a first lower ceramic ball layer 51, a second lower ceramic ball layer 52 and a third lower ceramic ball layer 53 below, the grain diameters of the three lower ceramic ball layers from top to bottom are respectively 6mm, 13mm and 19mm, and the heights of the three lower ceramic ball layers are respectively 200mm, 230mm and 200 mm. A first metal layer 31 (metal net) with a pore size of 14 meshes is arranged between the catalyst bed layer 20 and the upper ceramic ball layer. The bird nest proppant 60 has a particle size of 45mm and a height of 640 mm. A support grid 70 is disposed below the bird nest proppant 60. A baffling layer 80 is arranged between the feed inlet 11 and the support grid 70, and the height of the baffling layer 80 is 600 mm.
The aromatic raffinate oil and hydrogen are fully mixed, enter from the bottom of the hydrogenation reactor 1, contact with a hydrofining catalyst, carry out hydrogenation reaction under the condition of hydrogenation reaction, saturate olefin in the aromatic raffinate oil, and after the reaction is finished, the aromatic raffinate oil is discharged from a discharge hole 12 at the top of the hydrogenation reactor 1. See table 2 for relevant parameters.
Example 2
This example is essentially the same as example 1 except that a different aromatic raffinate feedstock is used. See table 2 for relevant parameters.
Comparative example 1
This comparative example is substantially the same as example 1, except that only one upper ceramic ball layer having a particle size of 6mm and a height of 200mm was disposed above the catalyst bed of the hydrogenation reactor, and the first metal layer, the second metal layer and the baffling layer were not disposed. In the hydrogenation process of the hydrogenation reactor, a top catalyst in the reactor has a leakage phenomenon, material flow has a bias flow and a channeling phenomenon, and a gas-phase dispersion phase is separated out at the top of the hydrogenation reactor to form a gas-phase space and a liquid level, so that the quality of a hydrogenation product is reduced. See table 2 for relevant parameters.
TABLE 2 Process conditions for hydrogenation and measurement results
| Item | Example 1 | Example 2 | Comparative example 1 |
| Aromatic raffinate oil raw material | |||
| Aromatic content, wt.% | 0.8 | 0.7 | 0.8 |
| Olefin content, wt.% | 5.2 | 4.9 | 5.2 |
| Process conditions of hydrogenation reactor | |||
| Reaction temperature of | 165 | 170 | 165 |
| Reaction pressure, MPa | 1.8 | 1.6 | 1.8 |
| Liquid hourly volume space velocity, h-1 | 6.8 | 6.5 | 6.8 |
| Oil quality | |||
| The olefin content in the aromatic raffinate oil after 48 hours of hydrogenation reaction is as follows by weight percent | 0.07 | 0.08 | 0.32 |
| Continuous operating cycle, month | 36 | 36 | 6~12 |
As can be seen from Table 2: adopt the utility model discloses a hydrogenation reactor can make the alkene content in the residual oil of arene be less than 0.1wt%, and the residual oil of arene is directly used as ethylene schizolysis's raw materials after the olefin takes off, can slow down the raw coke rate of schizolysis boiler tube, and the stable operation of ethylene cracker is guaranteed in the extension decoking cycle. Furthermore, the utility model discloses a continuous operation cycle of hydrogenation ware can show the extension.
The foregoing descriptions of specific exemplary embodiments of the present invention have been presented for purposes of illustration and description. It is not intended to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain certain principles of the invention and its practical application to enable one skilled in the art to make and use various exemplary embodiments of the invention and various alternatives and modifications as are suited to the particular use contemplated. Any simple modifications, equivalent changes and modifications made to the above exemplary embodiments shall fall within the scope of the present invention.
Claims (15)
1. An upflow liquid phase hydrogenation reactor, comprising:
the feeding hole is arranged at the bottom of the hydrogenation reactor;
the discharge hole is arranged at the top of the hydrogenation reactor;
a catalyst bed disposed within the hydrogenation reactor;
the first metal layer is arranged above the catalyst bed layer, the first metal layer is a metal net and/or a metal grid, and the aperture of the first metal layer is smaller than the particle size of the catalyst in the catalyst bed layer;
the upper ceramic ball layers are arranged above the first metal layer, and the particle size of each upper ceramic ball layer is gradually increased from bottom to top;
the second metal layer is arranged below the catalyst bed layer and is a metal net and/or a metal grid;
the lower ceramic ball layers are arranged below the second metal layer, and the particle size of each lower ceramic ball layer is gradually increased from top to bottom; and
and the baffling layer is arranged between the lower ceramic ball layers and the feed inlet.
2. The hydrogenation reactor according to claim 1, wherein the wall of the hydrogenation reactor is provided with an upper agent discharge port at the plurality of upper ceramic ball layers.
3. The hydrogenation reactor according to claim 1, wherein the wall of the hydrogenation reactor is provided with a lower agent discharge port at the plurality of lower ceramic ball layers.
4. The hydrogenation reactor according to claim 1 wherein the wall of the hydrogenation reactor is provided with a central unloading port at the catalyst bed.
5. The hydrogenation reactor according to any one of claims 1-4, further comprising:
and the support grid is arranged between the lower ceramic ball layers and the baffling layer.
6. The hydrogenation reactor of claim 5 further comprising:
a bird nest proppant disposed between the plurality of lower ceramic ball layers and the support grid.
7. The hydrogenation reactor of claim 6 further comprising:
and the third metal layer is arranged between the support grid and the bird nest propping agent, and the third metal layer is a metal net and/or a metal grid, and the aperture of the third metal layer is smaller than the particle size of the bird nest propping agent.
8. The hydrogenation reactor according to any one of claims 1-4 wherein the plurality of upper ceramic sphere layers are three layers.
9. The hydrogenation reactor according to claim 8, wherein the particle sizes of the three upper ceramic ball layers are respectively 4-7 mm, 10-14 mm and 16-20 mm from bottom to top, and the ratio of the heights of the three upper ceramic ball layers to the height of the catalyst bed layer is respectively (0.15-3.0): 10. (0.15-3.0): 10. (0.15-3.0): 10.
10. the hydrogenation reactor according to any one of claims 1-4 wherein the plurality of lower ceramic sphere layers are three layers.
11. The hydrogenation reactor according to claim 10, wherein the particle sizes of the three lower ceramic ball layers are respectively 4-7 mm, 10-14 mm and 16-20 mm from top to bottom, and the ratio of the height of the three lower ceramic ball layers to the height of the catalyst bed layer is respectively (0.15-3.0): 10. (0.15-3.0): 10. (0.15-3.0): 10.
12. the hydrogenation reactor according to any one of claims 1-4, wherein the pore size of the first metal layer is smaller than the particle size of the plurality of upper ceramic sphere layers; the aperture of the second metal layer is smaller than the particle size of the catalyst in the catalyst bed layer, and the aperture of the second metal layer is smaller than the particle size of the lower ceramic ball layers.
13. The hydrogenation reactor according to claim 12, wherein the first metal layer has a pore size of 12 to 16 mesh and the second metal layer has a pore size of 12 to 16 mesh.
14. The hydrogenation reactor of claim 13 wherein the catalyst in the catalyst bed has a particle size of less than 12 mesh.
15. The hydrogenation reactor of claim 1 wherein said first metal layer is disposed on said catalyst bed.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113262527A (en) * | 2021-05-26 | 2021-08-17 | 中国石油化工股份有限公司 | Export collection device and fixed bed reactor of developments defoaming |
| CN114471377A (en) * | 2020-10-28 | 2022-05-13 | 中国石油化工股份有限公司 | Reforming produced oil olefin removal reactor and reaction method |
| CN115501681A (en) * | 2021-06-23 | 2022-12-23 | 中国石油化工股份有限公司 | Adsorption tank, filter device and working solution online purification system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114471377A (en) * | 2020-10-28 | 2022-05-13 | 中国石油化工股份有限公司 | Reforming produced oil olefin removal reactor and reaction method |
| CN113262527A (en) * | 2021-05-26 | 2021-08-17 | 中国石油化工股份有限公司 | Export collection device and fixed bed reactor of developments defoaming |
| CN115501681A (en) * | 2021-06-23 | 2022-12-23 | 中国石油化工股份有限公司 | Adsorption tank, filter device and working solution online purification system |
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